;***************************************************************************** ;***************************************************************************** ;** NREL PROTECTED INFORMATION ** ;***************************************************************************** ;***************************************************************************** ; ; NREL Biomass to Ethanol Process ; NREL Protected Information ; Best Case Cofermentation (4_96a.INP) ; Modified to include the NREL Biofuels Databank of Physical Properties ; Authors: Vicky Putsche, Bob Wooley, Mark Ruth, Kelly Ibsen ; Date: April 26, 1996 ; ; Changes ;----------------------------------------------------------------------- ; I0203I.inp 20 March 2002; KNI 2002 design report final model ; 1. Changed temps of CSL, DAP and Cellulase 300 streams to 20 C. ; 2. BIOMASS define stmts from MIXED to CISOLID. ; 3. Remove negative sign from CO2 calc in FEEDPROP. ; 4. Added IF/ELSE stmt and negative sign to CEXTR calc to catch a ; negative COD and calculate a positive one from a neg. O2 coeff. ; 5. Added CEXTR, CPRO, CSOLS to CODCALC1, 2, END as READ VARS. ; 6. Moved AERAIR after CODCALC2 in sequence. ; 7. Changed 219 calculation in fortran RECYCLE to calculate solids in T310 ; per M. Ruth discussion to control solids in sacch. tank for agitation. ; 8. Made changes to MASSFLOW block per B. Atherton's work on E balance. ; 9. Overliming area changes per B. Hames, 3/22/02. ; Removed lignin ppt reaction from T-224; not likely at pH 9. ;10. Changed S-505 splits in block and fortran to send CSL, CNUTR, WNUTR ; to WWT, since they should be consumed by this point in process. All ; other solubles are treated as water. ;11. Updated 804 flow rate guess in stream statment - BRNAIR not converging. ; No help. Increased range for BNDLOW and BNDHI by changing 0.9 to 0.8 ; on BNDLOW and 1.0 to 1.2 on BNDHI. ;12. Updated QCD501, QRD501, QCD502, QRD502 inital values from stand alone ; distillation model run DM0203C.bkp. ;13. Removed several commented out lines to clean up code. ;14. Changed conversions in seed ferm F301F1-6 to match F300F but with 4% ; cell growth and added conversions for arabinose, mannose, galactose. ;15. Changed zymo, glycerol, lactic, etc. conversions in F300F to match ; Yellow Poplar data reported in the 2002 design case (EPD0005 run). ;16. Added statements in MASSFLOW to print out the calculated molecular ; weights of the soluble solids, extract, & protein components. (JLJ 5/10/02) ;17. Added work streams for DAP and DAP/CSL mixing: ; WC755 DAP solids feeder copy of WC225 ; WP755 DAP unloading blower copy of WP223 ; WP760 CSL/DAP pump copy of WP720 ; WT760 CSL/DAP day tank agitator 0.5 hp/1000 gal ;18. Moved 531 to M803MIX so that O2 for burner is calculated right. ; This will also fix BTU calculation (puts 531 into 803). ;19. Added stream 251 to block T914 to make PFDs look more balanced. ; Still not completely balanced since minor components that would be ; coming from RW stream 905 are not calcd. for streams 574,906,941. ;20. Changed WP211 calc to be based on FMP211 & FCP211 ;21. Added CH4101 & CH4840 definitions to COMBHEAT ;22. Removed TTL311, TTL31A, TTL303, & TTL304 from CNC2B calc in RECYCLE ;23. Changed HHVs of Soluble Solids, Proteins, & Extractives in COMBHEAT ; to be read as parameters 7, 8, & 9 from FEEDPROP ;24. Changed LHVs of Soluble Solids, Proteins, & Extractives in COMBHET2 ; to be read as parameters 10, 11, & 12 from FEEDPROP ;BGA1. Modified hard coded heat of combustion values in COMBHET2 in order ; to match heat of combustion values calculated for the energy balance. ; See Fortran Block COMBHET2 with initials BGA for edits. ;BGA2. Fortran block COMBHET2 -> Added the vaporization energy instead of ; subtracting because all the heats of combustion are negative. ; Significantly changed LHV of feed to combustor. ;----------------------------------------------------------------------- ; I0203G.inp 12 March 2002; KNI 2010 case parameters ; 1. Cost year from 1999 to 2000. ; 2. Feedstock cost from $35 to $30. ; 3. Increased from 85% to 90% PT yields for xylan, arabinan, galactan, mannan. ; Furfural down from 7.5% to 5%. Same for arabiinan, galactan, mannan. ; 4. Ferm time down from 2 to 1.5 days. ; 5. Ferm temp up from 37 C to 41 C in all blocks for ferms. ; No chilled water needed, QH14BSP to 0.000001 and CHW capital in EQUIP zero. ; 6. Increased ethanol from glucose from 92% to 95% in F300F. ; Took by-product reactions from comments for I0105A below. ; 7. CONTSPLT from 5 to 3%. ; 8. Mannose and galactose to ethanol yields to 85% in F300F. ; Took by-product reactions from comments for J0107E below. ; 9. Moved QH301 from CHW block to HEATCW-S. Reduced LB on CHWFLOW. ;10. Increased enzyme loading to 12 FPU/g in ENZ2 to get $0.10/gal. ;11. Change U value of H244 to 150 to reflect vapor/liquid heat transfer. ; Was 250. Changed H244 in equipment database to be like H-201, not H-200. ;12. Lowered soluble lignin conversin in M202HI to 5% (from P021207CS#2 run) ; that matches the State of Technology case. ;----------------------------------------------------------------------- ; I0203F.inp 12 March 2002; KNI New feedstock composition ; 1. Changed feedstock comp. in FEEDSTK and FEEDPROP to average of 2 ; BMAP batches received by NREL. ;----------------------------------------------------------------------- ; I0203E.inp 9 March 2002; KNI Separate Saccharification and Fermentation ; 1. Removed F301-6H block and moved/renamed SSFSPT/SACCHSPT to after F300H. ; Commented out seed cellulase calculations in fortran ENZYME. ; 2. H301 is now hyd. heater before sacch. tanks, and H302 is cooler for ; saccharified slurry to seed and production ferms. ; 3. Removed ENZ2S, stream 316 and 316 variables in FORTRAN STORE. ; 4. Moved 310 (DAP) and 310A (CSL) to F301-6F. ; 5. Added mixer FERMMIX to get CSL and DAP calculated before CONTSPLT. ; Can't use stream out of ferms for DAP calc due to gases that cause ; density to be low. ; Stream 304A is stream out of FERMMIX and used in FERMCSL and FERMDAP. ; 6. Added mixer SEEDMIX to get CSL and DAP calculated before F301-6F. ; Stream 303A is stream out of SEEDMIX and used in FERMCSL and FERMDAP. ; 7. Changed FORTRAN ENZ2 to calculate cellulase (312) from stream 301A. ; 8. Changed F300H to T310. Agitators for T310 are A310 with power WT310. ; Added pump P310 with power WP310 to transfer sacch.slurry to ferms. ; 9. Removed QF300A from SSCFCW and moved to HEATCW-S to remove from well ; water and CHW calcs. ; 10. Added list of PARAMETERS in use immediately before code starts ; 11. Renamed BTU101 from PARAM 30 to PARAM 4 ; 12. Renamed SSFVES from PARAM 4 to PARAM 31 ; 13. Removed COMMON RXCON (previously, it had been commented out) ; 14. Removed FRMSET & set the following params, renamed PUMPFLO to ; PMPSSF and column name from PUMPFLOW to PUMPSSCF in sensitivity: ; SSFDAY 32 ; SSFVOL 33 ; SSFWV 34 ; PMPSSF 35 ; 15. Removed CLSSET & set the following params ; CLYLD 41 ; CLPROD 42 ; CLVES 43 ; CLVOL 44 ; CLWV 45 ; 16. Added params for Saccharification calcs to param list after comments ; and to fortran SETVAR: ; SACVES 36 ; SACDAY 37 ; SACVOL 38 ; SACWV 39 ; PMPSAC 40 ; 17. Added work calculation for sacch. agitators, WT310. Based on WT300. ; 18. Added work calculation for sacch. transfer pump, WP310. Based on WP310. ; 19. Checked area 300 work calculations for correct streams. ; 20. Checked fortran RECYCLE and RECCOND for correct streams. ; 21. Changed conversion cellulose to glucoligs from 0.068 to 0.04 to match data ; in T310. ; 22. Removed SSFDAY,SSFVOL,SSFWV,PMPSSF and SACDAY,SACVOL,SACWV,PMPSAC from ; sensitivity block - not useD in Excel. ; 23. Added new equipment in database and checked streams:A-310,H-310,P-310,T-310. ;----------------------------------------------------------------------- ; I0203D.inp; 9 March 2002; KNI Fixes found from writing design report ; 1. Changed H200 temp spec from 40 C to 50 C. Since IX no longer in, match ; T209 (overliming) temp. ; 2. Since blowdown is now at 1 atm (more vapor), changed specs on H201- to ; include T spec of 95C. Moved QH201B to outlet of H201- and inlet of ; H201+B so it is calculated from T=95C spec on 501. ; 3. Due to sacch. temp., needed to heat slurry to sacch. up to 65C in H302. ; Added H302+ with steam stream 590, condensate 591. 590 in LPSTMD fortran. ; Design spec SACCHHEAT with QH302EX set to zero. Removed QH302 from HEATCW-S. ; Probably not reasonable to run overliming and gypsum sep at 65C, but ; maybe if S/L is out? ; 4. Added cooler H244 back in to cool stream 520 TO 30C before going to WWT. ; 5. Removed QT209XS, injection steam 237 and design spec HT-T209, since 240 is ; now 50 C, no extra heat needed in T209. ; 6. Matched steam temps up with process steams. ;----------------------------------------------------------------------- ; I0203C.inp; 1 March 2002; KNI Model PneumaPress vent stream to burner ; 1. Added condenser, H205 as FLASH2 to stream 260 out of PneumaPress to ; condense water. Specified T=38 (10 degrees higher than CW) and delta P=0. ; Added CW load, QH205 to block HEATCW-S, condensate stream 262 to S600. ; Get down from 10% moisture to 4%. ; Added area calculation in sensitivity MASSFLOW. ; 2. Vent stream from S505 is about the same moisture content as stream 804. ; No condenser on this one. ; 3. Add vent streams 261 and 560 to 804 with M802MIX. ; Adjusted design spec COMBAIR to include 261 and 560 in excess O2 calc. ;----------------------------------------------------------------------- ; I0203B.inp; 1 March 2002; KNI Model PneumaPress air/solids contact ; See 2002 stover design report for description of PneumaPress operation. ; 1. Added flash tank S205FLSH after S205B to model contact if air with solids ; after washing in PneumaPress unit. ; Changed solids stream exiting S205B from 255 to 255A. ; 2. Added flash tank S505FLSH after S505 to model contact of air with solids ; in PneumaPress unit. ; Changed solids stream exiting S505 from 571 to 571B. ; Changed vary stmt in design spec CFUGE3S from 571 to 571B. ; Changed fortran CFUGESLD stmts from 571 to 571B. ; Added S505FLSH to SEQUENCE 12. ;----------------------------------------------------------------------- ; I0203A.inp; 1 March 2002; KNI Changes to ESP Process Case ; 1. Decreased xylan to tar conversion in M-202 from 5% to 0, since not ; measured in experiments. ; 2. Increased xylan to furfural conversion in M-202 from 2.5% to 7.5% ; to account for degradation product formation that was tar. ; 3. Lowered soluble lignin yield in M202 from 30% to 15% since removing ; the hot wash. ; 4. Changed the cellulose to glucose in M-202 from 6% to 7%, which is ; supported with data and is 7% in the State of Tech case. ; 5. Removed hot wash; ambient washing separation like A0103A. ; COST EFFECT IS ABOUT $0.03/gal. ; Commented out (but left code in) H241+/-, H242+/-, H243+/-, T223, P228. ; from Aspen and Excel EQUIP sheet. ; Commented out design specs STM-241, HT-S254. ; Commented out heat streams QH241, QH241EX, QH242, QH243, QH244. ; Commented out WP228 and work calculation in FORTRAN PUMPS. ; 6. Changed stream input to S205SPT from 219A to 219. ; 7. Changed P spec in T203 from 5 to 1. ; 8. Commented out stream 265A and stream variable in FORTRAN LPSTMD. ; 9. Removed ratio in EQUIP sheet for S-205 higher pressure model. ;10. Changed stream 501A out of H201- to 501 and in area calc for H201. ;----------------------------------------------------------------------- ; I0202A.inp; 24 February 2002 Updated ESP Process Case ; 1. Changed description on ARFSH1 and 2 to COOLER... from PRESSURE ; REDUCER... ; 4. Renamed ARFSH1 and 2 to M205COOL and M505COOL, respectively. ; 5. Changed S205A and S205B pressure spec from 5.01 and 5.0 to .0. ; 6. Added Properties stmt to S205A to use NRTL-HOC, since 221 is part V without it. ; 7. Redefined BTU101 as parameter 30 (paramter 13 was already being used) and added ; the define statement to MASSFLOW to get HIHV0101 to show up. ; 8. Commented out NUMDRY calculation, since no dryer before burner. ; 9.Changed air receiver names and equip numbers, moved to area 900: ; T-215 now T-902 Pretreatment Pressure Filter Press Air Receiver ; T-507 now T-905 Product Recovery Pressure Filter Press Air Receiver ;----------------------------------------------------------------------- ;A0201F.inp; 22 February 2002. Updated ESP Process Case ; 1. Changed M-241 to T-241 in aspen, excel, and Database. Also m-242 ; to t-242 ; 2. Deleted P219, service not needed, including WP219 ; 3. Stream 219 now enters block H242- and stream 219B no longer exists ; 4. Added WP228, pumps filtrate blowdown from T223 to H200 and beyond. ; Based on P209 (and WP209). ; 5. Added AWP209 to Write-vars for PMPWK ; 6. Added stream 223L to excel sensitivity list so that P228 can be ; sized from it. ; 7. Add agitator to CSL storage tank (T720), named A720. Work stream ; will be WT720. It will be costed on A301. ;----------------------------------------------------------------------- ;A0201E.inp; 20 February 2002. Updated ESP Process Case ; 1. Added FeedProp fortran block to automatically calculate physical ; properties given the feedstock dry mass fractions and corresponding ; ultimate analysis. This eliminates the need for ; hhvfeed_cornstover_average_for_20yr_outlook.xls. ; 2. Make sure that stream 101, composition in FEEDPROP, and composition ; in FEEDSTK all match up. ; 3. Added '&' connectors for reactions 27, 36,and 37 for M803CMB RSTOIC ; They were not present, and the continuation lines didn't make it ; into the mass balance. ; 4. Changed initial guess for QH801 from 23. to 0.765. ; 5. At some point in time M803CMB reactions 27,36,37 went back to ; producing NO2 instead of N2 like was done starting in A0102L. ; this is done to control NOx emissions. ; 6. Therefore, changed reaction stoiciometry for reactions 27,36,37: ; coefficient for O2 changed from 1.19358 to 1.56672 ; NO2 changed to N2 and coefficient changed to 0.18657 ; 7. Changed definition of BNDLOW for COMBAIR to: ; F BNDLOW = 1 ;----------------------------------------------------------------------- ;A0201D.inp; 19 February 2002. Updated ESP Process Case ; 1. Added fortran FEEDSTK from M0108W ; 2. Added Feedstk fortran block to automatically calculate the flow of ; soluble solids, protein, extracts and CI solid streams. This ; eliminates the need for Stream 101 Calculation Round 2.xls. ;----------------------------------------------------------------------- ;A0201C.inp; 15 February 2002. Updated ESP Process Case ;1. Fix error in calculation of Area for H241: ; Replace T219E w/ T219A. (change in MESP of $0.0002) ;2. Equate LP steam temperatures: ; Changed temperature in initial guesses for streams 215, 237, 265A, ; 592, 594, 596, & 815 from 167.9566 to 163.5110. ;----------------------------------------------------------------------- ;M0201A.inp; 16 January 2002. Updated A0201A.inp to be able to work with ; new Excel macros ;1. Added: PROP-SET CP1 CPMX SUBSTREAM = MIXED ; PROP-SET CP2 CPMX SUBSTREAM = CISOLID ; PROP-SET FRAC MOLEFLOW SUBSTREAM = MIXED PHASE = L V ; PROP-SET COMP1 MASSFLOW SUBSTREAM = MIXED ; PROP-SET COMP2 MASSFLOW SUBSTREAM = CISOLID ; STREAM-REPOR MASSFLOW PROPERTIES=CP1 CP2 FRAC COMP1 COMP2 ;2. Eliminated unnecessary variables from the MASSFLOW sensitivity block. ; A variable was considered unnecessary if it was not calculated in ; the sensitivity block and was already written to the report file. ;3. Removed P501GP from FERMSET and set it as PARAMETER #5 ;4. Modified Process Equipment database for new stream title methodology ;---------------------------------------------------------------------- ;A0201A.inp; 02 January 2002. Fixes to ESP case before creating 2010 case ; 1. Add stream 253 (STRM0253) to sensitivity MASSFLOW. A-241 is ; scaled from it. ; 2. Changed column label in MASSFLOW from STRM0250 to STRM0252 for ; defined variable S252. ; 3. Add stream 219 (STRM0219) to sensitivity MASSFLOW. P-219 is ; scaled from it. ; 4. Add fortran to calculate sum of streams 221 & 256 in MASSFLOW ; (similar to streams 510 and 521) ; F S22156 = S221 + S256 ; 5. Renumbered the Tabulate statements in MASSFLOW to add spacings. ; 6. Changed high pressure steam leaving turbine from 5.5 to 13 atm ; (stream 216, stream 814, m811htrb) ; 7. Take out T-222; no longer needed. Delete streams 218A and 223. ; Now sending stream 256 to T-223. ;---------------------------------------------------------------------- ;A0112G.inp; 31 December 2001. Fixes to ESP case before creating 2010 case ; 1. Added QH244 to HEATCW-S. ;---------------------------------------------------------------------- ;I0112C.inp; 28 December 2001. Fixes to ESP case before creating 2010 case ; Y indicates the changes are in this model; N indicates they are still ; to be made in later models, namely the 2010 $1.07 case to be published. ;Y1. Removed T spec on H201- because enthalpy across H201+/H201- was ; out of balance; not enough heat in QH201+QH201B to get to 95C. ;Y2. Also moved QH201 to outlet of H201+A, and inlet of H201- becuase ; for this situation (not enough heat available), it should be an input ; heat stream, not a calculated heat required stream. ;Y3. Put 501 (as 501A) through H243+/- to get some heat from 242B. ; Set T spec of H243- to 84 C. to get a >=10 C delta between 501A and 520A. ; VFRAC=0 spec will not work due to CO2 in stream; puts T at 53, which ; causes a T cross. Rest of heat is going to CW to get T=30(?) (not V=0, ; which would require the CO2 to be condensed). ; There is a deficit of heat to get 501 to 95 now that the T203 flash is ; at 5 atm - about half the vapor volume than at 1 atm flash. ; Final cooling of 242B to make its temperature compatible for waste water ; treatment now done in H244. ; Area calculations for H243 & H244 corrected. ;Y4. Minor changes to spreadsheet (Equipment, Heat and Work) to ; correct OLE links. ;Y5. Checked Equipment database against EQUIP sheet. Refreshed data, ; which caused a new M-202 cost (with Alloy-825) to come into EQUIP. ; MESP increased by $0.01. Changed scaling stream for T-224/A-224 ; back to 239 in database - AA or MR did not remember changing. ;N6. Need to decide whether to remove area 400 or let calculate to 0. LEAVE IN ;Y7. Remove zeroed items in EQUIP and OPCOST in Excel. ;Y8. Correct M-202 cost - using ratio for lower temp than ESP param sheet shows. ;Y9. Added block ARFSH1 (modeled after AFLSH) to reduce TEMPERATURE ONLY of ; pneumapress air. Input stream = 258, output streams=259,QM205 ; QM205 is input to HEATCW-S because cooling water will be used. ; Added block ARFSH2 for 2nd pneumapress. New streams are 259 and ; QM505. Cooling water is also used. ;Y10. Removed Spec 3, Vary 1 statment from D501 per J.Jechura tech memo. ; Changed mole-rr from 7 to 3. ;N11. Removed commented out lines. ;Y12. Corrected MULDIP for xylitol - wrong number in it. ;N13. Make steam stream 860 consistent with other indirect steams (592, 594). ; Use heat stream and fortran block, not material stream. ;N14. Clean up/document fortran calcs for M-202, M-107, M-104. ;N15. Decide which new spreadsheets to put into the std and full Excel workbooks. ;N16. Use different RW to wash stover? Evap is the cleanest. ;N17. Area 100 power calcs are hard to manipulate. ;Y18. Generate new PFDs for ESP process case, P105 ;N19. Generate new PFDs for 2010 case, P110 ;Y20. Add new process numbers to equipment database for P105 and P110 equipment ;N21. Try to write errror handler for H201- temp cross with stream 218. ;Y22. Made sure that the loop checking for recycle water greater than makeup was ; in fortran CHEMICAL. ;---------------------------------------------------------------------- ; J0109C.INP; 26 September 2001. Sensitivities to NEP Stage 3 Process Case: ; modified plant size. ; 1. Adjust the component rates in Stream 101 to hit 2,000 dry tonnes/day & ; 85% solids. ; 2. Increased upper limit on ACIDCONC to 10000. Added PARAM MAXIT=500 to ; TEAR2. ; 3. Increased pressure of S205A to 5.01 atm to prevent vaporization of ; stream 221. ; 4. Decreased contamination from 7% to 5%. ;---------------------------------------------------------------------- ; J0109B.INP; 07 September 2001; NEP Stage 3 Process Case. Conditions as ; specified in 06 September 2001 meeting. ; 1. Modify hydrolysis conditions. Changed xylose yields to 85%, consistent ; with the I0104A NEP Target Case. Kept soluble ligning yield the same (30 ; wt%). Hydrolysis conditions changed to 1.1 wt% H2SO4 @ 190�C for 2 min. ; Reactor solids concentration (CONC1 in FORTRAN RECCOND) slightly changed ; 0.3091 -> 0.30. ; Specific pre-hydrolysis yields (M202HI) are: ; CONV 5 CISOLID XYLAN 0.025 --> 0.025 ; CONV 6 CISOLID XYLAN 0.95 --> 0.85 ; CONV 7 CISOLID XYLAN 0.0125 --> 0.025 ; CONV 8 CISOLID XYLAN 0.0125 --> 0.05 ; CONV 9 CISOLID MANNAN 0.025 --> 0.075 ; CONV 10 CISOLID MANNAN 0.95 --> 0.85 ; CONV 11 CISOLID MANNAN 0.025 --> 0.075 ; CONV 12 CISOLID GALACTAN 0.025 --> 0.075 ; CONV 13 CISOLID GALACTAN 0.95 --> 0.85 ; CONV 14 CISOLID GALACTAN 0.025 --> 0.075 ; CONV 15 CISOLID ARABINAN 0.025 --> 0.075 ; CONV 16 CISOLID ARABINAN 0.95 --> 0.85 ; CONV 17 CISOLID ARABINAN 0.0125 --> 0.0375 ; CONV 18 CISOLID ARABINAN 0.0125 --> 0.0375 ; 2. Modify fermentation conditions. Changed SSFDAY (SSCF residence time) to ; 3.5 (1.5 day hydrolysis + 2 days fermentation). Adjusted the conversion ; of Cellulose -> Glucose (F300H, rxn #3) to 90% to get an overall ; conversion of Cellulose -> Ethanol of 82.8%. The other 2 reactions were ; also scaled. ; CONV 1 CISOLID CELLULOS 0.019 --> 0.068 ; CONV 2 CISOLID CELLULOS 0.003 --> 0.012 ; CONV 3 CISOLID CELLULOS 0.978 --> 0.9 ; 3. Add reaction to OL process to allow a portion of the soluble lignin to ; precipitate out with the gypsum. Added reaction & its conversion to T224: ; STOIC 2 MIXED LGNSOL -1.0 / CISOLID LIGNIN 1.0 ; CONV 2 MIXED LGNSOL 0.50 ; 4. Modified corn stover composition to match that used in R0109C. ; Specifically: ; a. Modified Stream 101 composition. ; b. Modified heat of formation (DHFORM) and composition info (NOATOM) for SOLSLDS, EXTRACT, ; & PROTEIN ; c. Modified M803CMB equations for SOLSLDS, EXTRACT, & PROTEIN (STOICH 27, 36, & 37). ; d. Modified the oxygen requirements for SOLSLDS, EXTRACT, & PROTEIN in ; CODCALC1, CODCALC2, CODEND (CSOLS, CEXTR, CPRO in each) due to ; stoichiometry changes. ; e. Changed the HHV of SOLSLDS, EXTRACT, & PROTEIN in COMBHEAT (HCSOL, ; HCEXT, HCPRO). ; f. Modified Stoichiometry in Equations 19, 47, 48, 31, 49, & 50 in T608 ; for new composition ; g. Modified lower heating values of SOLSLDS, EXTRACT, & PROTEIN in ; COMBHET2 (CMBSOL, CMBEXT, CMBPRO). ;---------------------------------------------------------------------- ; J0107E.INP; 13 July 2001; Super Stover Target Case. Hydrolysis & Fermentaton ; conditions similar to NEP Target Case (I0104A). ; 1. Modify hydrolysis & fermentation conditions. Increase hydrolysis ; temperature to 65�C (H302 & F300H). Increase fermentation temperature to ; 37�C (F300F, F300CONT, H301, F301-6H, & F301-6F). Changed enzyme loading ; (ELOAD) from 15 to 10. Changed SSFDAY (SSCF residence time) to 3 (1 day ; hydrolysis + 2 days fermentation). Reduced chilled water fraction from ; 20% to 10% (reduced QH14BSP from 0.2 -> 0.1). Changed Arabinose yields ; in F300F: ; CONV 26 MIXED ARABINOS 0.0 --> 0.85 ; CONV 27 MIXED ARABINOS 0.0 --> 0.029 ; CONV 28 MIXED ARABINOS 0.0 --> 0.002 ; CONV 29 MIXED ARABINOS 0.0 --> 0.015 ; CONV 30 MIXED ARABINOS 0.0 --> 0.024 ; CONV 31 MIXED ARABINOS 0.0 --> 0.014 ;---------------------------------------------------------------------- ; J0107D.INP; 12 July 2001; Super Stover with 90% Xylose yields. ; 1. Increased pretreatment yields (M202HI) of xylose, mannose, glactose, & ; arabinose to 85%. Specific yields are: ; CONV 5 CISOLID XYLAN 0.075 --> 0.025 ; CONV 6 CISOLID XYLAN 0.85 --> 0.95 ; CONV 7 CISOLID XYLAN 0.0375 --> 0.0125 ; CONV 8 CISOLID XYLAN 0.0375 --> 0.0125 ; CONV 9 CISOLID MANNAN 0.075 --> 0.025 ; CONV 10 CISOLID MANNAN 0.85 --> 0.95 ; CONV 11 CISOLID MANNAN 0.075 --> 0.025 ; CONV 12 CISOLID GALACTAN 0.075 --> 0.025 ; CONV 13 CISOLID GALACTAN 0.85 --> 0.95 ; CONV 14 CISOLID GALACTAN 0.075 --> 0.025 ; CONV 15 CISOLID ARABINAN 0.075 --> 0.025 ; CONV 16 CISOLID ARABINAN 0.85 --> 0.95 ; CONV 17 CISOLID ARABINAN 0.0375 --> 0.0125 ; CONV 18 CISOLID ARABINAN 0.0375 --> 0.0125 ;---------------------------------------------------------------------- ; J0107C.INP; 11 July 2001; Super Stover with 85% Xylose yields. ; 1. Restored oligimer hold tank. Re-installed block T222 & streams 218A & ; 223. Stream 256 now inlet to T222 & 223 fed to T223. Power for A-241 ; re-installed in Fortran block POWER. In spreadsheet, added costs for ; A-241, H-241, T-261, T-262, M-241, & M-242 back into sheet EQUIP. ; 2. Increased pretreatment yields (M202HI) of xylose, mannose, glactose, & ; arabinose to 85%. Specific yields are: ; CONV 5 CISOLID XYLAN 0.05 --> 0.075 ; CONV 6 CISOLID XYLAN 0.75 --> 0.85 ; CONV 7 CISOLID XYLAN 0.1 --> 0.0375 ; CONV 8 CISOLID XYLAN 0.05 --> 0.0375 ; CONV 9 CISOLID MANNAN 0.05 --> 0.075 ; CONV 10 CISOLID MANNAN 0.75 --> 0.85 ; CONV 11 CISOLID MANNAN 0.15 --> 0.075 ; CONV 12 CISOLID GALACTAN 0.05 --> 0.075 ; CONV 13 CISOLID GALACTAN 0.75 --> 0.85 ; CONV 14 CISOLID GALACTAN 0.15 --> 0.075 ; CONV 15 CISOLID ARABINAN 0.05 --> 0.075 ; CONV 16 CISOLID ARABINAN 0.75 --> 0.85 ; CONV 17 CISOLID ARABINAN 0.1 --> 0.0375 ; CONV 18 CISOLID ARABINAN 0.05 --> 0.0375 ; ;---------------------------------------------------------------------- ; J0107A.INP; 11 July 2001; Super Stover Base Case ; 1. Modifications for possibility of stream 840 as biomass to boiler. (Most ; of these were left commented out, though.) ; a. Copied stream 101 biomass definition to stream 840. Left commented out. ; b. Revised FORTRAN FLOW840 to directly calculate the substream flows ; from the Stream 840 definition. Left commented out. ; c. Modified calculation in O2CALC to determine O2 requirement for biomass ; to boiler. ; d. Modified definition of WATCON to include water & CISOLID from Stream ; 840 (consistent with R0005E). ; e. Modified the calculations of HLE840 & WATCON (in COMBHET2) to properly ; take into account the biomass as feed to the boiler. ; f. Modified the calculation of the HHV of 840 in COMBHEAT. ; g. Added the flowrate to the MASSFLOW sensitivity block. ; 2. Added stream values to MASSFLOW to be able to do a steam balance & energy ; analysis in the spreadsheet. Made the following changes in the spreadsheet: ; a. In the GetSens VBA function increased dimension of HNAMES from 1540 -> 3000 ; & increased length of HEADER from 13000 to 26000. ; b. Added VBA modules Module_Steam32 & Module_CallableRoutines to do direct ; steam table calculations. ; c. Added sheets "Steam Balances", "Energy & Heat Contents", & "Energy Analysis". ; d. In sheet "OPCOST" added cell I1 to calculate last row of "aspen" range & ; modified cells G2 & H2 to use this value. ; 3. Start of Super Stover changes. Oligomer hold removed. Block T222 & streams ; 218A & 223 removed; stream 256 routed to inlet of H200. Removed power for ; A-241 from Fortran block POWER. In spreadsheet, zeroed out costs for ; A-241, H-241, T-261, T-262, M-241, & M-242 on sheet EQUIP. ; 4. Hot wash in Pneumapress. Oulet temperature of H241- adjusted with Design ; Spec (HT-S254) to make separation temperature (stream 254 out of S205MIX) ; 135�C. Pressures of S205A & S205B increased from 1 to 5 atm. ; Prehydrolysis blowdown tank (T203) spec changed to 5 atm pressure (from ; 135�C). ; 5. Pretreatment reactor at 180�C & 0.7 wt% acid. Change temperature in ; M202HI to 180. Change specification in ACIDCONC to 0.007. Set M202HI ; conversions back to FY01 Benchmark case values except for ; Cellulose -> Glucose & Lignin -> Soluble Lignin: ; CONV 3 CISOLID CELLULOS 0.065 --> 0.06 ; CONV 6 CISOLID XYLAN 0.90 --> 0.75 ; CONV 7 CISOLID XYLAN 0.025 --> 0.1 ; CONV 8 CISOLID XYLAN 0.025 --> 0.05 ; CONV 10 CISOLID MANNAN 0.90 --> 0.75 ; CONV 11 CISOLID MANNAN 0.05 --> 0.15 ; CONV 13 CISOLID GALACTAN 0.90 --> 0.75 ; CONV 14 CISOLID GALACTAN 0.05 --> 0.15 ; CONV 16 CISOLID ARABINAN 0.90 --> 0.75 ; CONV 17 CISOLID ARABINAN 0.02 --> 0.15 ; CONV 18 CISOLID ARABINAN 0.02 --> 0.055 ; CONV 23 CISOLID LIGNIN 0.05 --> 0.30 ; 6. SSCF reactor 4 days @ 32�C. Changed hydrolysis temperatures (H302 & ; F300H) to 32; changed fermentation temperatures (F300F, F300CONT, H301, ; F301-6H, & F301-6F) to 32. Changed enzyme loading (ELOAD) from 10 to ; 15. Changed SSFDAY (SSCF residence time) to 4. Revised the fermentation ; conversions to match FY01 NEP Benchmark case: ; CONV 7 MIXED GLUCOSE 0.95 --> 0.92 ; CONV 8 MIXED GLUCOSE 0.019 --> 0.027 ; CONV 9 MIXED GLUCOSE 0.001 --> 0.002 ; CONV 10 MIXED GLUCOSE 0.006 --> 0.008 ; CONV 11 MIXED GLUCOSE 0.015 --> 0.022 ; CONV 12 MIXED GLUCOSE 0.009 --> 0.013 ; CONV 16 MIXED XYLOSE 0.95 --> 0.85 ; CONV 17 MIXED XYLOSE 0.017 --> 0.029 ; CONV 18 MIXED XYLOSE 0.001 --> 0.002 ; CONV 19 MIXED XYLOSE 0.004 --> 0.006 ; CONV 20 MIXED XYLOSE 0.005 --> 0.009 ; CONV 21 MIXED XYLOSE 0.014 --> 0.024 ; CONV 22 MIXED XYLOSE 0.009 --> 0.014 ; CONV 26 MIXED ARABINOS 0.95 --> 0.0 ; CONV 27 MIXED ARABINOS 0.017 --> 0.0 ; CONV 28 MIXED ARABINOS 0.001 --> 0.0 ; CONV 29 MIXED ARABINOS 0.009 --> 0.0 ; CONV 30 MIXED ARABINOS 0.014 --> 0.0 ; CONV 31 MIXED ARABINOS 0.009 --> 0.0 ; CONV 35 MIXED GALACTOS 0.95 --> 0.0 ; CONV 36 MIXED GALACTOS 0.017 --> 0.0 ; CONV 37 MIXED GALACTOS 0.001 --> 0.0 ; CONV 38 MIXED GALACTOS 0.009 --> 0.0 ; CONV 39 MIXED GALACTOS 0.014 --> 0.0 ; CONV 40 MIXED GALACTOS 0.009 --> 0.0 ; CONV 44 MIXED MANNOSE 0.95 --> 0.0 ; CONV 45 MIXED MANNOSE 0.017 --> 0.0 ; CONV 46 MIXED MANNOSE 0.001 --> 0.0 ; CONV 47 MIXED MANNOSE 0.009 --> 0.0 ; CONV 48 MIXED MANNOSE 0.014 --> 0.0 ; CONV 49 MIXED MANNOSE 0.009 --> 0.0 ; Wanted an overall conversion of Cellulose -> Ethanol of 90%. Adjusted ; the conversion of Cellulose -> Glucose (F300H, rxn #3) to 97.8%. The ; other 2 reactions were scaled so that the total conversion of Cellulose ; does not exceed 100%. ; CONV 1 CISOLID CELLULOS 0.068 --> 0.019 ; CONV 2 CISOLID CELLULOS 0.012 --> 0.003 ; CONV 3 CISOLID CELLULOS 0.9 --> 0.978 ; 7. Restored contamination loss to 7%. Changed CONTSPLT from 0.03 -> 0.07. ; 8. Restored chilled water fraction to 20%. Changed QH14BSP from ; 0.000000001 to 0.2. ; 9. Added blowdown tank (T223) to the Pneumapress filtrate. Liquid (223L) ; sent to overliming & vapor (223V) sent to heat recovery (H242+) on ; recycle water (H242-). There is more heat available than can be ; recovered; the exit steam is condensed (H243) & sent on to waste water ; treatment. Added pump (P219) to bring recycle water up to 5 atm. ; 10. Modified streams used for heat exchanager areas to account for ; re-routed streams. ; a. Changed inlet stream for calculation of A200 from 221 to 223L. ; b. Changed inlet stream for A241 from 219 to 219C. ; c. Added area calculations for H242 (similar to A241) & H243 (similar ; to H200). ;---------------------------------------------------------------------- ; I0105A.inp; 11 May 2001; Year 2010 case for FY01 Annual Outlook ; Remove IX ; Y1. Removed IX by removing sequence SEQ9 ; Y forts IXRGNFLW, PREACID -- Modified OLIME to read stream 240 not 236 ; Y & 0'd costs of S-221, A-202, P-225&6, A-235 ; Y Removed STORE vars AMFLW1 (242) & AFLOW3 (235) ; Y CHEMICAL var FLWIX3 (243) ; Y PUMPS calcs & vars for P-225 & P-226, IX power calc. ; Y WATERDEM var FLIX3 ; Y also removed blocks A202, S221A, S221B, & A235, and ; Y streams 242, 243, 244, 245 (from E501SPT, too), 241, 246, 247 ; Y (from S600, too), 235, 236 (from T209, too - changed to 240) ; Y3. Added stoichiometric flow to the liming factor in OLIME to neutralize ; the acid in stream 240 (more now, since no IX to remove it). ; N4. Made 230 the outlet of T224 ; Y5. Made 240 an inlet to T209 ; Y1. Changed ACIDCONC from 0.5% to 0.35%. ; Y2. Changed enzyme loading from 15 FPU/g to 10 FPU/g to get $0.08/gal. ; Y3. Added capital costs for oligomer hold tank/lining/agitator T241/T242/A241. ; Y -added power for A241 to fortran POWER. ; Y4. Added capital for second flash tanks (T221/T222) after olig hold. ; Y5. Changed cost of M202 in EQUIP based on lowered pressure at 150 C. ; Y6. Reduced SSFDAY from 7 to 3 ; Y7. Increased F300H Cellulose-->Glucose from 0.8 to 0.9 ; Y8. Modified the following F300F Yields ; Reaction Old New ; Glucose-->Ethanol 0.92 0.95 ; Glucose-->Zymo 0.027 0.019 ; Glucose-->Glycerol 0.002 0.001 ; Glucose-->Succinic Acid 0.008 0.006 ; Glucose-->Acetic Acid 0.022 0.015 ; Glucose-->Lactic Acid 0.013 0.009 ; Xylose-->Ethanol 0.85 0.95 ; Xylose-->Zymo 0.029 0.017 ; Xylose-->Glycerol 0.002 0.001 ; Xylose-->Xylitol 0.006 0.004 ; Xylose-->Succinic Acid 0.009 0.005 ; Xylose-->Acetic Acid 0.024 0.014 ; Xylose-->Lactic Acid 0.014 0.009 ; Arabinose-->Ethanol 0.85 0.95 ; Arabinose-->Zymo 0.029 0.017 ; Arabinose-->Glycerol 0.002 0.001 ; Arabinose-->Succinic Acid 0.015 0.009 ; Arabinose-->Acetic Acid 0.024 0.014 ; Arabinose-->Lactic Acid 0.014 0.009 ; Galactose-->Ethanol 0.0 0.95 ; Galactose-->Zymo 0.0 0.017 ; Galactose-->Glycerol 0.0 0.001 ; Galactose-->Succinic Acid 0.0 0.009 ; Galactose-->Acetic Acid 0.0 0.014 ; Galactose-->Lactic Acid 0.0 0.009 ; Mannose-->Ethanol 0.0 0.95 ; Mannose-->Zymo 0.0 0.017 ; Mannose-->Glycerol 0.0 0.001 ; Mannose-->Succinic Acid 0.0 0.009 ; Mannose-->Acetic Acid 0.0 0.014 ; Mannose-->Lactic Acid 0.0 0.009 ; Y9. Reduced CONTSPLT from 0.07 to 0.03 ;Y10. Increased pretreatment yields from 75% to 90% (Xylan, Mannan, Galact, Arab). ; Decreased Furfural and tar yields from 5% to 2.5% for xylan, arabinan. ; Decreased HMF yields from 10% to 5% for mannan, galactan. ;Y11. Changed QH14BSP from 10% to 0.000000001. ;Y12. Changed H301, F300F, F300CONT, F301-6F, F301-6H temp. from 30 to 41 C. ;Y13. Changed feedstock cost from $35 to $30 per ton. ;Y14 Changed M202 MOC from alloy 825 to SS316 using 1/1.19 Harris factor. ;Y16. Added heat exchanger H241 to preheat wash water for S-205. ; -Added area calculation for H241 ; -Added steam stream 265A to heat RW ; -Added design spec STM241 to control steam flow ; -Added stream 265A to fortran LPSTMD ; 1. No data for oligomer conversion - added to justify keeping the same ; yields in M202 at lower acid and temp - so no block for now, only cost. ; Y2. Added second flash step (would be after olig hold) T-222 to 1 atm. ; Y3. Changed T-203 to T spec to get 135 C for olig hold step. ; Y5. For now, combined flash vapor stream 218A from T-222 with that ; from T-203 going into H201+A. Probably some waste heat integration ; opportunities with evap. ; Y6. Added streams 218A and 223. ; 7. Increase UB on SCRBFLOW from 20000 to 40000. ; 8. Increased UB on VLPSTM from 50000 to 500000. ; 9. Lowered steam pressure of HP turbine from 13 to 5.5 atm. ;---------------------------------------------------------------------- ; A0103A.inp; 28 MARCH 2001; Design Case for Process Design Update 2001 ; 1. Consolidated all air compressor requirements into two compressors ; for the plant instead of 6 separate ones (4 for pneumapresses and ; 2 for plant air). Kept this as M904 but created a new equipment ; cost for it via ICARUS. Cellulase air compressor (M401) still ; kept separate but since it's not currently used, it doesn't matter ; 2. Relabeled WM904 as WM904A. ; 3. Added block AIRCMP (mixer block) to sum plant and instrument air ; and pneumapress air requirements. Outflow stream is now WM904. ; Inlet flows are WM205, WM505, WM904A. Disconnect WM205 from ; MPOW2, WM505 from MPOW5, and WM904A from MPOW10. ; 4. Define new work stream WM904. ; 5. Connected stream WM904 to inlet of MPOWTOT. ; 6. Eliminate M-205 and M-505 compressors from equipment list in ; excel. ;---------------------------------------------------------------------- ; A0102T.inp; 27 MARCH 2001; Design Case for Process Design Update 2001 ; 1. Moving post-distillate separation equipment from Area 600 to ; Area 500. ; 2. Relabel the following equipment: A-630, C-601, M-605, P-630, ; S-605, T-605, T-630 to A-530, C-501, M-505, P-530, S-505, T-507, ; T-530 ; 3. Relabel Material Streams: 600 to 570, 601 to 571, 601A to 571A, ; 602 to 572, 603 to 573, 604 to 574, 606 to 576, 610 to 580, ; 657 to 557, 658 to 558. ; 4. Relabel Work streams: WC601, WM605, WP630, WS605, WT630 to WC501, ; WM505, WP530, WS505, WT530. ; 5. Added block MPOW5 to Area 500 to sum up the miscellaneous work ; requirements for area 500. Created new work stream WMP5. Added ; the following streams to this block: WC501, WM505, WS505. ; 6. Added block MPOW5 to Sequence SEQ11. ; 7. Renamed block S601 to S505. ; 8. Moved following blocks to area 500: DCOOL2, S505, T530, M505, ; FWMIX, RWSPLT ; 9. Made changes to excel spreadsheet and Access database as well. ; 10. Renamed propane storage tank T708P to T709 to stick with ; convention. Done in excel and access. ;---------------------------------------------------------------------- ; A0102S.inp; 07 MARCH 2001; Design Case for Process Design Update 2001 ; 1. Added cellulase enzyme storage tank (T-750) in excel and P-750 ; also. Sized for 48 hr residence time, P-750 copy of P-713 because ; it had the closest flowrate. ; 2. Added work stream WP750 for cellulase pump. Modeled after WP720. ; 3. Removed WP212 & P-212 & T-212 from costs ; 4. Removed WP227 ; 5. Added WM205, WP205, WP211, & WP213 to A200 work summary calc. ; 6. Changed pressure of S205A & S205B from 5 to 1 atm ; 7. Added S-103 magnet separator cost ; 8. Added WS103 for magnet separator with 0.0 power requirement (like ; R0008B). ;---------------------------------------------------------------------- ; A0102R.inp; 26 Feb 2001; Design Case for Process Design Update 2001 ; 1. Added work stream WP205 back in for pneumapress feed pump as part ; of design. ; 2. Added agitation work stream WT205 for hydrolysate mixing tank ; agitator (prior to pneumapress, mixes hydrolysate and dilution ; recycle water). Modeled after WT232. Added wt205 to flowsheet, ; DEF-STREAMS WORK, stream definition initial guess. ; 3. Added calculation of WT205 to FORTRAN POWER, modeled as WT232 ; calculation. Variables labeled HMT instead of SLT. ; 4. Calculation for WT205 in FORTRAN POWER based on stream 220 ; 5. Also included WT205 in SENSITIVITY next to WT232. ; 6. Added capital costs into excel (via database) for A-205 ; (same as A-232), T-205, and P-205. ; 7. Also changed enzyme cost from $0.08/gal to $0.15/gal in database. ; 8. Added spared (in database) for P-101, P-102, P-103, P-104, ; P-105, P-205, P-211, P-212, P-213, & M-102 ;---------------------------------------------------------------------- ; A0102Q.inp; 26 Feb 2001; Propane instead of diesel for forklift ; 1. Added propane to pure components. (C3H8) ; 2. Replaced BCDF variable in FORTRAN STORE with BCPF for Base Case ; Propane Flow. ; 3. Set BCPF = 14.97 kg/hr based on 33 lb propane tank lasting 8 hrs ; and 8 forklifts required ; 4. Changed initial guess for stream 723 from DENAT component to ; propane and flow from 203.7 to 14.97. ; 5. Changed DP708 in Fortran PUMPS from 51.6 to 0.0 because propane ; won't be pumped out of its storage tank. ; 6. Excel changes: set # required and # spares for P-708 to 0 & 0. ; 7. Added propane tank to process equipment database as T708P. ; 8. Changed T708 in EQUIP to T708P for propane. ; 8. Changed diesel flow in Opcost sheet (S-3) to S-12, which is ; propane. ;---------------------------------------------------------------------- ; A0102P.inp; 21 Feb 2001; Other model changes for design update ; 1. Excel changes only - Changed cost year to 1999 and updated ; INDICES and raw materials costs in DB. ;---------------------------------------------------------------------- ; A0102O.inp; 21 Feb 2001; Other model changes for design update ; 1. Changed kgO2/kg component ratio for soluble lignin from 2.6529 ; to 1.6000. This number was experimentally verified by Evergreen ; analytical. ;---------------------------------------------------------------------- ; A0102N.inp; 21 Feb 2001; Other model changes for design update ; 1. Changed block H201+ into two blocks: H201+A, H201+B, connected ; by stream 222. ; 2. Changed spec for block H201+A to PRES=0.0 VFRAC=1.0 ; 3. Spec for block H201+B is PRES=0.0 VFRAC=0.0 ; 4. Left QH201 connected to block H201+A. ; 5. Added QH201B heat stream for block H201+B. ; 6. Added QH201B heat stream to def-streams heat. ; 7. Connected QH201B with H201- ; 8. Changed calculation for A201 as sum of required areas for sensible ; and latent heat changes. ;---------------------------------------------------------------------- ; A0102M.inp; 21 Feb 2001; Other model changes for design update ; 1. Changed block H811- into two blocks: H811-A, H811-B, connected ; by stream 819. ; 2. Changed spec for block H811-A to PRES=-0.68 VFRAC=0.0 ; 3. Left QH811 connected to block H811-A ; 4. Changed spec for block H811-B to PRES=0.0 VFRAC=0.0 ; 5. Added QH811B heat stream for block H811-B ; 6. Added QH811B to def-streams heat. ; 7. Changed VFRAC in H811-A from 0.0 to 1.0 ; 8. Connected QH811B with H811+. ; 9. Changed calculation for A811 as sum of required areas for ; sensible and latent heat changes. ;---------------------------------------------------------------------- ; A0102L.inp; 21 Feb 2001; Other model changes for design update ; 1. Added stream 311 back into FORTRAN RECYCLE. This stream was ; mistakenly labeled as a CSL stream before when it was NH3. It ; should have been CSL. Now, it is DAP, which needs to be included. ; 2. Stream 311A was also added to FORTRAN RECYCLE. This is the CSL ; stream that needed to be included in the first place. ; 3. Changed temperature of stream 524 from 55F (13C) to 26C to match ; stream 904 temp. ; 4. Changed temperature of stream 943 from 28C to 26C to match stream ; 904 temp. ; 5. NO2 emissions from boiler were too high because of addition of ; soluble components: PROTEIN and EXTRACT. Therefore, to enable ; FORTRAN POLLUTE to model NOx production correctly, we must change ; the stoichiometry for reactions 27,36 and 37 in M803CMB. ; 6. Changed reactions 27,36,37 to produce N2 instead of NO2. ; Stoichiometry now looks as follows: ; STOIC 27 MIXED SOLSLDS -1.0 / O2 0.68755 / H2O 0.27007 / & ; CO2 1.0 / N2 0.12615 / SO2 .00181 ; 7. Added the following DEFINE statement to FORTRAN WATERDEM: ; DEFINE CIPCS STREAM-VAR STREAM=906 SUBSTREAM=MIXED & ; VARIABLE=MASS-FLOW ; 8. Added CIPCS to write-vars in WATERDEM to set flowrate of stream ; 906. ; 9. Changed calculation in SCRBFLOW for 40 ton/yr. Changed 8000 hr/yr ; to 8406 hr/yr to match what's being used in excel. This changes ; SPEC from 4.536 to 4.316. ; 10. Commented out DNH3 variable in FORTRAN STORE. Stream 717 is now ; calculated as sum of NH3 in streams 242, 434, 436 only. ; 11. Changed seed fermentor nutrient loadings to 2x production nutrient ; loadings (.5% CSL, 0.67 g/L DAP in FERMCSL and FERMDAP) ;---------------------------------------------------------------------- ; A0102K.inp; 19 Feb 2001; Anco-Eaglin Continuous Reactor used ; 1. Added calculation in Sensitivity block to determine the number of ; Anco-Eaglin reactors required. Based on calculation to determine ; required number of centrifuges. May not want to use it for Anco, ; however, could be used for Andritz Quote. ; 2. Changed work requirement for WM202 from 1363 HP to 1801 HP to ; match Anco-Eaglin quote. 85% of motor sizes assumed power usage ; same as previous reactor quote. (1741 HP was listed in Harris ; report, however original quote HP added up to 1801, see app. F). ; 3. Anco-Eaglin quote is for SS316L paddles, not alloy 825. The ; increased utility cost to exchanging SS316L paddles for 825 is ; minimal because the densities of each material are similar. ; Dens SS316L=8.03 g/cm3, A825=8.14 g/cm3 ; 4. According to Harris report, cost factor between A825 and SS316L ; for Anco-Eaglin is 1.19. Original quote was for SS316L paddles. ; Increased cost for A825 paddles will be included in the estimate ; in the database. ;---------------------------------------------------------------------- ; A0102J.inp; 19 Feb 2001; Fermentation mass balance revisited ; 1. In order to enable the control blocks FERMCSL and FERMDAP to work ; changed the stoichiometry of reactions 8,36,45 in blocks F300F and ; F301-6F. ; 2. Started with old equation: ; STOIC 8 MIXED GLUCOSE -1.0 / NH3 -1.2 / ; CISOLID ZYMO 6.0 / MIXED H2O 2.4 / ; MIXED O2 0.3 ; 3. Replaced 1.2 NH3 w/ corresponding (on mass basis) CSL and DAP ; since that is what's actually used in NREL experiments. ; 4. Used a CSL to DAP ratio of 7.6 (2.5 g/L / 0.33 g/L) ; 5. By molecular weight difference, 20.43 g CSL + DAP required per ; mole glucose: ; 20.43 * 7.6/8.6 = 18.05 g CSL / 18.015 g/mol = 1.00 mol CSL ; 20.43 * 1.0/8.6 = 2.38 g DAP / 132.056 g/mol = 0.018 mol DAP ; 6. Reactions 8,36,45 then become: ; STOIC 8 MIXED GLUCOSE -1.0 / CSL -1.0 / DAP -0.018 / ; CISOLID ZYMO 6.0 / MIXED H2O 2.4 / ; MIXED O2 0.3 ; 7. Changed DAP requirement in seed fermentors from 10 g/L to 2 g/L ; This is 6x the requirement in the production fermentors, similarly ; as is was done for CSL. ; 8. Same logic used to obtain the following for reactions 17,27 of ; blocks F300F and F301-6F: ; STOIC 17 MIXED XYLOSE -1.0 / CSL -0.835 / DAP -0.015 / ; CISOLID ZYMO 5.0 / MIXED H2O 2.0 / ; MIXED O2 0.25 ;---------------------------------------------------------------------- ; A0102H.inp; 19 Feb 2001; Edit Fermentation Mass Balance ; 1. Changed reactions 17,27 in F300F and F301-6F to: ; STOIC 17 MIXED XYLOSE -1.0 / CSL -1.0 / DAP -0.5 / ; CISOLID ZYMO 5.0 / MIXED H2O 3.75 / ; MIXED O2 1.36 ; 2. Added DAP requirements to FORTRAN STORE. DAP requirement is sum ; of streams 310, 311. Sets flow of stream 755. ; 3. Added stream 755 to flowsheet to TSTORE block. Also added initial ; guess for stream 755 of 1000 kg/hr. ; 4. Added streams 755, 310, 311 to sensitivity block. ;---------------------------------------------------------------------- ; A0102G.inp; 16 Feb 2001; Edit Fermentation Mass Balance ; 1. Added FORTRAN FERMDAP to set flowrate of DAP into seed and ; production fermentors. Modeled after FERMCSL. ; 2. Set DAP addition rate at 0.33 g/L for production fermentor per ; Nancy Dowe's recommendation. ; 3. Set DAP addition rate at 10.0 g/L for seed fermentor. This was ; necessary for sufficient material to satisfy the mass balance in ; the fermentors. (may want to look at this further in the future) ; 4. Set initial guesses for streams 310, 311 at 500 kg/hr ;---------------------------------------------------------------------- ; A0102F.inp; 16 Feb 2001; Edit Fermentation Mass Balance ; 1. Changed reactions 17,27 in F300F and F301-6F to: ; STOIC 17 MIXED XYLOSE -2.0 / CSL -1.0 / DAP -1.0 / ; CISOLID ZYMO 10.0 / MIXED H2O 6.5 / ; MIXED O2 2.71 ;---------------------------------------------------------------------- ; A0102E.inp; 16 Feb 2001; Edit Fermentation Mass Balance ; 1. Changed fermentation mass balance to eliminate need for ammonia. ; Ammonia was used strictly for mass balance purposes but it not ; really used in the actual fermentation. CSL is actual nitrogen ; source. ; 2. Commented out initial guesses for streams 310, 311. Also comment ; them out in FORTRAN STORE and sensitivity block. ; 3. Deleted streams 310,311 from F301-6H and F300H in flowsheet. ; 4. Deleted stream 311 and all references from FORTRAN RECYCLE ; 5. Commented out FORTRAN NUTRC and FORTRAN NUTR300. ; 6. Changed NH3 component in blocks F300F, F301-6F to CSL. ; 7. Added pure component Diammonium Phosphate (DAP) to components list ; MW is 132.056 (NH4)2HPO4 ; 7. Changed reactions 8, 36, 45 in F300F and F301-6F to: ; STOIC 8 MIXED GLUCOSE -1.0 / CSL -1.0 / DAP -0.6 / ; CISOLID ZYMO 6.0 / MIXED H2O 4.3 / ; MIXED O2 1.63 ; This was done making sure that C balanced, then N, then H, used ; O2 coefficient to make up the difference in MW to make MW of ; each side of the reaction balance. ; 8. Changed streams 310, 311 from NH3 to DAP and uncommented. Set ; initial guess at 5500 kg/hr. Added back into flowsheet also. ;---------------------------------------------------------------------- ; A0102D.inp; 16 Feb 2001; Switch to USRAN4 w/ prot,extr,sollgn ; 1. Added protein, extractives and soluble lignin to USRAN2 subroutine ; and renamed it USRAN4. ; 2. Changed COD ratio in CODEND for LGNSOL from 5.3058 to 2.6529. ; 2.6529 is the correct kgO2/kg component requirement for lignin w/ ; molecular composition C10 H13.9 O1.3 ;---------------------------------------------------------------------- ; R0102C.inp; 9 Feb 2001; Minor Design Case Modifications ; 1. Broke out Income Tax from Return on Investment on Summary Sheet ; 2. Increased number of yard employees from 8 to 32 per Harris Sub. ; 3. Renamed WM106 to WM107 & set requirement to 25 kW ;---------------------------------------------------------------------- ; R0102B.inp; 8 Feb 2001; Added Purchase Cellulase Flow and Cost ; 1. Added 312 (cellulase) as inlet to F300H & as feed stream ; 2. Added FORTRAN block ENZ2 to set flows of 312 ; 3. Modified RECYCLE to include 312 in calcs ; 4. Added 316 (cellulase) as inlet to F301-6H & as feed stream ; 5. Added FORTRAN block ENZ2S to set flows of 316 ; 6. Added 750 as inlet to TSTORE (total cellulase requirement) ; 7. Calculated 750 flow with STORE ; 8. Added 750 to Sensitivity ; 10. Added Cellulase Cost as R-7 to Database to be $0.08/gal ; in 1999$ ;----------------------------------------------------------------------- ; R0102A.inp; 8 Feb 2001; Removed Cellulase Production Cost ; 1. Reduced ENZYL & ENZYLS to 0.0000001 ; 2. Zeroed out A400 equipment costs (EQUIP) ;-------------------------------------------------------------------- ; R0101F.inp; 8 Feb Y2K; Post-Dist Pneumapress solids reduced to % ; 1. Modified CFUGE3S to reach 45% water in 601 instead of 88% solids ;------------------------------------------------------------------ ; R0101E.inp; 1 Feb Y2K; Post-Dist Pneumapress ; 1. Changed CFUGE3S's spec from 0.3 to 0.88 ; 2. Reduced lower bound on CFUGE3S ; 3. Included CSL, GLUCOSE, & CNUTR in CFUGE3S calc so most goes ; with solids but still allows solids conc to be reached ; 4. Commented out DRYSTM ; 5. Set flow of 853 to 0.0000001 ; 6. Added compressor M605 & 657 & 658 & WM605 ; 7. Added SOLD600 & STRM0657 to sensitivity ; 8. Renamed WS601 to WS605 & modified calc in MISCPOW ;------------------------------------------------------------------ ; R0101B.inp; 24 Jan Y2K; Pneumapress Comparison ; 1. Renamed S202 to S205A & CT-S202 to CT-S205A ; 2. Changed CT-S205A's spec from 0.4 to 0.548 (match insoluble ; solids in Pneumapress Test #9) ; 3. Added S205SPT to set flow of recycle water to S205 (also ; added 252 & 253) ; 4. Added S205WASH to set flow of 252 & 257 ; 5. Added S205MIX to mix 225 & 252 into 254 ; 6. Added S205B with inlet 254 separated into cake 255 and ; filtrate 256 & CT-S205B to set splits ; 7. Added S205SOL to set the flow of solubles in 256 and get proper ; overall solubles recovery ; 8. Added 255 & 253 as inlets to C202 ; 9. Added M205, 257, 258, & WM205 to set air flow for pneumapress ; 11. Removed P100 from C-202 old DB entry (#82) ; 12. Added new DB entries for C-202,P-205,S-205,T-211,P-211,T-212, ; P-212,T-213,P-213,M-205,t-215 (#537-547) ; 14. Added P-205,S-205,T-211,P-211,T-212,P-212,T-213,P-213,M-205, ; T-215 to EQUIP ; 15. Removed Cost of S-202 on EQUIP ; 16. Added 256 & 257 to sensitivity ; 17. Removed P-205 cost because P-211 & C-201 should be sufficient ; 18. Removed cost of P-227 from EQUIP ; 19. Set WS205 Requirement in MISCPOW ; 20. Set WC202 Requirement in MISCPOW ; 21. Added WP205 as input with calculation in PUMPS and then set its ; power to 0 because it is not used in NREL's design ; 22. Added WP211 as input with calculation in PUMPS ; 23. Added WP212 as input with calculation in PUMPS ; 24. Added WP213 as input with calculation in PUMPS ; 25. Set WP227 to 0.0 in PUMPS ;--------------------------------------------------------------------- ; R0011B.inp; 17 Nov Y2K; Base Case -- Stover Feedstock & Aspen 10.2 ; 1. Fixed WRITE statement in CFUGE3S ; 2. Fixes to COMBHET2 ; Fixed CMBCLB definition ; Changed X2SACN in calculation to CMBX2S ; Added definition for WAT803 ; 3. Fixes to COMBHEAT ; Changed HC615 statements to proper components in BTU615 calc ; Removed Calc of FRC620 because 620 no longer fed to boiler ; Added Definition of SOL531 ; 4. Fixes to O2CALC ; Added ROC, RODEN, ROEXS, & ROUNK values ; 5. Fixes to CODCALC1 ; Corrected XACI in calculation to XLACI ; 6. Fixes to NUTR300 ; Added definition of ZNH302 ; 7. Fixes to RECYCLE ; Changed CSLCONC value to be used instead of commented out ; Changed RCLS to RCSL in calculation ; Changed CFI2 to CFS1 in calculation ; Changed CFCLS to CFCSL in calculation ; Changed CPI2 to CPS1 in calculation ; Changed CPCLS to CPCSL in calculation ; Changed CLI2 to CLS1 in calculation ; Changed CLCLS to CLCSL in calculation ; Changed SFI2 to SFS1 in calculation ; Changed SFCLS to SFCSL in calculation ; Changed SPI2 to SPS1 in calculation ; Changed SPCLS to SPCSL in calculation ; 8. Used ; to comment out EPM103 in POW101 instead of c because line ; was too long and caused errors ; 9. Removed SSFVES from COMMON and made it PARAM 4 & added to POWER & ; PUMPS read/write vars ; 10. Added more read-vars to PUMPS to make it a complete list ;---------------------------------------------------------------------- ; R0011A.inp; 3 Nov Y2K; Base Case -- Stover Feedstock Handling ; 1. Removed the following work streams from simulation & MISCPOW: ; WC103, WC106, WC107, WC108, WM101, WS103, WW101 ; 2. Removed sawdust work streams from simulation & MISCPOW: ; WC151, WC152, WC154, WM151, & WM153 ; 3. Removed FTYPE (param 1) -- Added 101 temp variable to SETVAR because ; a variable needs to be sampled to allow simulation to run ; 4. Added POW101 as input block and moved following work calcs to it: ; WC101, WC102, WC104, WC103, WM104, WS101, WS102 from MISCPOW ; WP101 from PUMPS ; 5. Added the following works to the process w/ calc in POW101: ; WM105, WP102, WP104, WM106, WP103, WP105 ; 6. Added 102 as outlet of E501SPT ; 7. Added FSPLIT C103 with outlets 102A and 104 ; 8. Added FSPLIT M104LOSS with outlets 102B and 103 ; 9. Added MIXER M104MIX with inlets 102B and 101 and outlet 105 ; 10. Changed inlet to M202MIX from 101 to 105 ; 11. Added POWER to SEQ11 ; 12. Added Polymer for settling and belt press: ; Renamed C103 to C103B ; Renamed 104 to 104B ; Added C103A (outlets 104A & 104D--into C103B) ; Added 107 (to sensitivity, too) & POLY1 to control its flow ; Added C103C to mix 104A & 104B making 104 ; Added polymer cost as S-11 to operating costs ; 13. Added all equipment to Basis with Equipment sizing spreadsheet & ; linked new info to Excel ; 14. Modified RECCOND to calculate water flows and splits ;----------------------------------------------------------------------- ; R0008B.inp; 17 Aug Y2K; Base Case ; 1. Changed the power requirement for P-224 in pumps (just found error) ; 2. Renamed FLSH601 to M801FLSH ; 3. Removed QM803AIR as inlet to M801FLSH ; 4. Added QM801 as inlet to M801FLSH ; 5. Removed 851 as inlet to M803AIR+ ; 6. Added M801CND & 852 & QM801B to condense flash vapors ; 7. Removed QM803AIR from convergence block TEAR2 ; 8. Added M801STM with 853 and 854 to provide heat for M801FLSH ; 9. Added D-Spec DRYSTM to set the flow of 853 ; 10. Added 853 to HPSTMD ; 10. Renamed M803AIR+ to H801+ ; 11. Added H801- and 804B and set QM803AIR destination to H801- ; 12. Renamed QM803AIR to QH801 & renamed in sens. block ; 13. Attached QM801B destination to HEATCW-S ; 14. Changed H-801 in Basis from Obsolete to not & set it to scale on QHET0801 ; 15. Made previous M-801 obsolete in Basis ; 16. Added new M-801 to Basis ; 17. Added NUMDRY (label NUMRDRYR) as number of dryers to sensitivity ; 18. Modified WM801 calc in MISCPOW to fit ReTec quote ; 19. Increased the Cost Factor for H-801 (burner air preheater) from 1.0 to 1.5 in ; Basis (1.5 is from Cran's work & Walas's reference of it) ; 20. Added Convergence Block BRNAIR to converge COMBAIR and QH801 simultaneously ; 21. Added 852 as inlet to E501WW ; 22. Added convergence blocks EV1SZ & EV2SZ and modified SEQ13 ;---------------------------------------------------------------------------------- ; R0008A.inp; 10 Aug Y2K; Base Case (no new dryer) ; 1. Corrected ACNBIO to BIO803 in COMBHET2 ; 2. Made Yard Employees Scale with Plant size (like the intracellular note says it does) ; 3. Removed worksheet name from GetSens macro ; 4. Changed Ethanol density for gal/yr calc (OPCOST!B78) from stream 703 to 515E ; 5. Set up OPCOST and EQIUP to read data from ASPEN rows 2 to 300 instead of 200 max ; 6. Imported Kelly's updated INDICES sheet and updated the following names to new cells: ; Capital_Index, Capital_Year, Chemical_Index, Chemical_Year, Labor_Index, Labor_Year ; 7. Adjusted Overhead/Maint. Cell Calculation to be based on cost year info instead of Base Year ; 8. Added O2CALC fortran to set upper & lower limits for COMBAIR ; 9. Copied the Sensitivity Block from M0007B.COSTFIG.INP ; 10. Increased the feedstock (F-1) cost in Basis to $35/dry ton (2000$) & updated ; query for Excel Basis worksheet ; 11. Imported Cost Breakdown by Area Data and Figs (including feedstock losses) from ; m0007b2.costfig.xls -- Made significant changes and named many cells in "old" ; worksheets ; 12. Added Steam and Electricity use calcs to Summary Sheet ; 13. Reorganized Summary Sheet ; 14. Corrected 809A statement in Sensitivity ; 15. Added 812D, 814, 815, & 860 to Sensitivity for steam use calc. ; 16. Changed base labor costs to 1998$ (previously '95 was probably wrong) ; 17. Removed 809A and added 804D to PFD-A801 ;-------------------------------------------------------------------------------- ; R0004B.inp; 5 April Y2K; Base Case w/ Average Corn Stover Composition ; 1. Modified Stream 101 to corn stover composition ; 2. Added heat of formation and composition info for SOLSLDS, EXTRACT, & PROTEIN ; 3. Modified M803CMB equations for SOLSLDS, EXTRACT, & PROTEIN ; 4. Modified the oxygen requirements for SOLSLDS, EXTRACT, & PROTEIN in ; CODCALC1, CODCALC2, CODEND ; 5. Changed the HHV of SOLSLDS, EXTRACT, & PROTEIN in COMBHEAT ; 6. Modified Stoichiometry in Equations 19, 47, & 48 in T608 for new composition ; 7. Modified Stoichiometry in Equations 31, 49, & 50 in T608 for new composition ; 8. Entered the lower heating values of SOLSLDS, EXTRACT, & PROTEIN in COMBHET2 ;-------------------------------------------------------------------------------- ; R0003F.inp; 10 March Y2K; 20 year outlook Base Case w/ Corn Stover ; 1. Reduced Water flow in 101 from 27778 to 14706 ; 2. Changed the LHV of lignin & unknown in COMBHET2 to -3.928E9 ;-------------------------------------------------------------------------------- ; R0003E.inp 8 March Y2K; 20 year Base Case w/ Corn Stover (high moisture) ; 1. Modified Stream 101 to corn stover composition ; 2. Added heat of formation and composition info for SOLSLDS, EXTRACT, & PROTEIN ; 3. Modified M803CMB equations for SOLSLDS, EXTRACT, & PROTEIN ; 4. Modified the oxygen requirements for SOLSLDS, EXTRACT, & PROTEIN in ; CODCALC1, CODCALC2, CODEND ; 5. Changed the HHV of SOLSLDS, EXTRACT, & PROTEIN in COMBHEAT ; 6. Modified Stoichiometry in Equations 19, 47, & 48 in T608 for new composition ; 7. Modified Stoichiometry in Equations 31, 49, & 50 in T608 for new composition ; 8. Entered the lower heating values of SOLSLDS, EXTRACT, & PROTEIN in COMBHET2 ; 9. Corrected errors in D501 with the following: ; 1) Increased the vapor rate upper limit in FRWD501 (D501VU) from a ratio ; of 1.2 to a ratio of 1.4 ; 2) Set the fraction of CO2 in the distillate to 0.845 from 0.836 ; 3) Made 510 be product of stage 3 instead of stage 4 ; 10. Set D502 calcs to match the stand-alone (RADFRAC) model ; 1) Changed the mole-frac EtOH in 511 from 0.824 to 0.826 ; 2) Changed the temp of 511 from 92.419 to 92.404 ; 3) Changed the temp of 516 from 120.74 to 120.91 ; 4) Changed the reboiler heat duty / feed flow ratio (REBFCT) from ; 7.10037E-5 to 6.74933E-5 in D502QCR ; 5) Changed the condensor heat duty / feed flow ratio (CNDFCT) from ; 3.527307E-4 to 3.94405E-4 in D502QCR ; 11. Added Extractives and Protein to Soluble Solids Calc. on AUTOCAD worksheet ; 12. Corrected Density Calc. Error on AUTOCAD worksheet ; 13. Added Both Components and fixed density error on WaterBal worksheet ;------------------------------------------------------------------------------- ; R0003D.inp; 8 March Y2K; Added Extractives and Protein ; 1. Added EXTRACT component as extractives in the mixed substream ; 2. Used same properties as soluble solids ; 3. Added EXTRACT to S221B, D502, S601, M803CMB, CFUGESLD, RECYCLE, ; CODCALC1, CODCALC2, CODEND, COMBHEAT & COMBHET2, T608 ; 4. Added EXTRACT to physical prop sets with VB, MULDIP, MUP & RGYR ; 5. Added PROTEIN component as protein in the mixed substream ; 6. Used same properties as soluble solids ; 7. Added PROTEIN to S221B, D502, S601, M803CMB, CFUGESLD, RECYCLE, ; CODCALC1, CODCALC2, CODEND, COMBHEAT & COMBHET2, T608 ; 8. Added PROTEIN to physical prop sets with VB, MULDIP, MUP & RGYR ; 9. Modified RECCOND to calculate SOLSLDs, EXTRACT, & PROTEIN as solids in ; prehydrolysis reactor ;-------------------------------------------------------------------------------- ; R0003C.inp; 7 March Y2K; New Base Case with Stoich and Recycle Errors Corrected ; 1. Changed the Molecular weight of glucolig to match cellulose (162.1424) from ; 162.115 ; 2. Changed the molecular weight of CELLOB to be 2*cellulose + water = 342.3001 ; from 342.2398 ; 3. Changed the Molecular weight of XYLOLIG to match XYLAN (132.11612) from ; 132.0942 ; 4. Changed the Molecular weight of TAR to XYLAN+water (150.1314) from ; 150.1040 ; 5. Changed the Molecular weight of MANOLIG to match cellulose (162.1424) from ; 162.115 ; 6. Changed the Molecular weight of GALAOLIG to match cellulose (162.1424) from ; 162.115 ; 7. Changed the Molecular weight of ARABOLIG to match XYLAN (132.11612) from ; 132.0942 ; 8. Changed ACETOLIG to use acetic acid properties not Acetate ; 9. Changed the stoichiometry for Biomass production in T608 for new MWs ; 10. Uncommented 401 params in RECYCLE ; 11. Removed Gibbs energy of formation for LGNSOL ;------------------------------------------------------------------------------- ; R0003B.inp; 6 March Y2K; New Base Case with Soluble Lignin ; 1. Added LGNSOL component as soluble lignin ; 2. Added reaction 23 to M202HI to convert LIGNIN to LGNSOL and set conversion ; at 5% (previous data shows 2% to 15%) ; 3. Added physical property info for LGNSOL ; 4. Added LGNSOL to M202HI, S221B, D502, S601, M803CMB, CFUGESLD, RECYCLE, ; CODCALC1, CODCALC2, CODEND, COMBHEAT & COMBHET2 ;------------------------------------------------------------------------------- ; R0003A.inp; 2 March Y2K; New Base Case ; 1. Removed commented out CONC1 calculation in RECYCLE (it is calculated in ; RECCOND) ; 2. Added additional RECYCLE printout info from R0002B1 ; 3. Modified the cost of F-400. It had used the miscalculation of 173352 + 600 = ; 179952 instead of 173352 + 600 = 173952. ; 4. Scaled Plant Staff Costs according to A. Aden memo addition dated 2 March 00 ; 5. Recosted T-306 & A-306 to 4 hour residence time per Bridge subcontracts ; 6. Changed residence tim for WT306 to 4 hours in POWER ; 7. Added cost of a spare beer column reboiler (H-501) ; 8. Set D-501 to scale on diameter squared (DI501) instead of diameter and ; recosted it and changed its scaling factor ; 9. Changed the scaling factor of D-502 to match D-501 ;-------------------------------------------------------------------------------- ; R0001A.inp; 4 Jan Y2K; New Base Case ; 1. Changed the Residence Time COMMENT for A-224 from 4 days to 4 hours in POWER ; 2. Added Residence time term to A-402 power calculation in POWER & modified ; comments ; 3. Corrected comment for S-601 in POWER ; 4. Corrected power requirement for T-306 in POWER ; 5. Corrected power requirement for WT300 in POWER ; 6. Changed comment on power requirement for WP300 ; 7. Changed WT602 basis from 618 to 612 in POWER ; 8. Corrected comments about WT606 ; 9. Added summary file name & date/time stamp to ASPEN worksheet ; 10. Added sort to Update Data routine on ASPEN worksheet ; 11. Changed the HHV of acetate and acetolig from 6469.6 to 14263.0 Btu/kg ; in COMBHEAT (6469.6 is Btu/lb and was incorrectly entered in R99012Y) ; 12. Completed Full Economic spreadsheet for use with model ; 13. Added carry loss forward calculation to default economic analysis worksheet ; 14. Updated Basis linked sheet ; 15. Updated all sheets that are used for PFDs and put them into .FULL.XLS file ;---------------------------------------------------------------------------------- ; *****PARAMETER VALUES IN USE***** ; 2 HLETOT ; 3 WATCON ; 4 BTU101 ; 5 P501GP ; 7 HCSOL ; 8 HCPRO ; 9 HCEXT ; 10 CMBSOL ; 11 CMBEXT ; 12 CMBPRO ; 13 CEXTR ; 14 CPRO ; 15 CSOLS ; 31 SSFVES ; 32 SSFDAY ; 33 SSFVOL ; 34 SSFWV ; 35 PMPSSF ; 36 SACVES ; 37 SACDAY ; 38 SACVOL ; 39 SACWV ; 40 PMPSAC ; ; 41 CLYLD ; 42 CLPROD ; 43 CLVES ; 44 CLVOL ; 45 CLWV ; ; 51 TOTWAT ; 52 WATPER ; 55 BNDLOW ; 56 BNDHI ;=========================================================================== ; Total Plant File ;=========================================================================== ; TITLE 'BIOMASS TO ETHANOL PROCESS: TOTAL PLANT **NREL PROTECTED INFO**' ; IN-UNITS MET TEMPERATURE=C OUT-UNITS MET TEMPERATURE=C ENTHALPY-FLO='MMKCAL/HR' MASS-ENTHALP='KCAL/KG' & MASS-ENTROPY='KCAL/KG-K' DEF-STREAMS MIXCISLD ALL DIAGNOSTICS HISTORY SYS-LEVEL=4 SIM-LEVEL=4 PROP-LEVEL=2 STREAM-LEVEL=4 RUN-CONTROL MAX-TIME=20000.0 MAX-ERRORS=4000 MAX-FORT-ERRORS=200 SYS-OPTIONS INTERPRET=NO HISTORY MAX-PRINT SIM-LIMIT=1000 ; SIM-OPTIONS PROP-DERIV=NUMERICAL ;Heat capacity PROP-SET CP1 CPMX SUBSTREAM = MIXED PROP-SET CP2 CPMX SUBSTREAM = CISOLID PROP-SET FRAC MOLEFLOW SUBSTREAM = MIXED PHASE = L V PROP-SET COMP1 MASSFLOW SUBSTREAM = MIXED PROP-SET COMP2 MASSFLOW SUBSTREAM = CISOLID ; CONV-OPTIONS SECANT BRACKET=YES WEGSTEIN MAXIT=100 QMAX=0.5 ; FLOWSHEET-REPORT NOTOTBAL NOFORTRAN NODESIGN-SPEC NOCOMPBAL NOCONVERGENCE ; NODESCRIPTION ; ; NODESCRIPTION Eliminates the Convergence Summary, but also gets rid of the ; flowsheet connectivity ; BLOCK-REPORT NOINPUT NOTOTBAL INCL-BLOCKS = M811ISPT D501 D502 & M811HTRB M811ITRB M811LTRB & M811VLRB & F400 F401-4 AFLSH & H501 ; ; Use EXCL-BLOCKS = or INCL-BLOCKS = to reduce the number of blocks reported ; STREAM-REPORT WIDE MASSFLOW NOZEROFLOW NOCOMP-ATTR NOSUBS-ATTR ; ; Use EXCL-STREAMS = or INCL-STREAMS = to reduce the number of blocks reported ; With Ion Exchange need to eliminate 10 streams from the report ; EXCL-STREAMS = 905 909 & ; 922 923 STREAM-REPOR MASSFLOW PROPERTIES=CP1 CP2 FRAC COMP1 COMP2 REPORT NOPROPERTIES ;PROPERTY-REPORT PARAMS ; ;=========================================================================== ; Components ;=========================================================================== ; COMPONENTS ; In-house database components GLUCOSE C6H12O6 GLUCOSE / CELLULOS C6H10O5 CELLULOS / XYLOSE C5H10O5 XYLOSE / XYLAN C5H8O4 XYLAN / LIGNIN CXHXOX-1 LIGNIN / CELLULAS CHXNXOXSX-2 CELLULAS / BIOMASS CHXNXOXSX-1 BIOMASS / ZYMO CHXOXNX ZYMO / UNKNOWN CXHOX UNKNOWN / SOLSLDS CHXOXSX SOLSLDS / EXTRACT CHXOXSX EXTRACT / PROTEIN CHXOXSX PROTEIN / GYPSUM CaSO4-2H2O GYPSUM / ACETATE C2H4O2-N1 ACETATE / ; In-house database aliases ARABINOS C5H10O5 ARABINOS / ; Use Xylose properties GALACTOS C6H12O6 GALACTOS / ; Use Glucose properties MANNOSE C6H12O6 MANNOSE / ; Use Glucose properties ARABINAN C5H8O4 ARABINAN / ; Use Xylan properties MANNAN C6H10O5 MANNAN / ; Use Cellulose properties GALACTAN C6H10O5 GALACTAN / ; Use Cellulose properties GLUCOLIG C6H12O6 GLUCOLIG / ; Use Glucose properties CELLOB C6H12O6 CELLOB / ; Use Glucose properties XYLOLIG C5H10O5 XYLOLIG / ; Use Xylose properties TAR C5H8O4 TAR / ; Use Xylan properties MANOLIG C6H12O6 MANOLIG / ; Use Glucose properties GALAOLIG C6H12O6 GALAOLIG / ; Use Glucose properties ARABOLIG C5H10O5 ARABOLIG / ; Use Xylose properties ACETOLIG C2H4O2-1 ACETOLIG / ; Use AAcid properties XYLITOL CXHOX XYLITOL / ; Use Xylose properties LGNSOL LGNSOL LGNSOL / ; Physical properties described below ; Solids Database CASO4 CASO4 CASO4 / CAH2O2 "CA(OH)2" CAH2O2 / ASH CAO ASH / ; Purecomps Database ETHANOL C2H6O-2 ETHANOL / H2O H2O H2O / FURFURAL C5H4O2 FURFURAL / HMF C5H4O2 HMF / H2SO4 H2SO4 H2SO4 / N2 N2 N2 / CO2 CO2 CO2 / O2 O2 O2 / CH4 CH4 CH4 / NO NO NO / NO2 NO2 NO2 / NH3 H3N NH3 / LACID C3H6O3-D1 LACID / AACID C2H4O2-1 AACID / NH4OH H3N NH4OH / NH4SO4 "(NH4)2SO4" NH4SO4 / NH4ACET "(NH4)2SO4" NH4ACET / GLYCEROL C3H8O3 GLYCEROL / SUCCACID C4H6O4-2 SUCCACID / DAP "(NH4)2HPO4" DAP / PROPANE C3H8 PROPANE / ; DENAT IS GASOLINE FOR DENATURING DENAT C7H16-1 DENAT / ; OIL IS CORN OIL FOR ANTIFOAM. OIL C18H34O2 OIL / CSL H2O CSL / ; CNUTR ARE CELLULASE NUTRIENTS (SALTS) AND WNUTR ARE ; NUTRIENTS FOR WASTEWATER TREATMENT (I.E. TRIPLE ; SUPER PO4 AND UREA). CNUTR H2O CNUTR / WNUTR H2O WNUTR / SO2 O2S SO2 / H2S H2S H2S / C C C / CO CO CO ; HENRY-COMPS HC O2 N2 CO2 CH4 ; ;=========================================================================== ; Physical Property Data ;=========================================================================== ; ; New Statements setting up the NREL Biofuels Database ; DATABANKS PURE93 / SOLIDS ;/ NOASPENPCD PROP-SOURCES INHSPCD / PURE93 / SOLIDS IN-HOUSE-DATA PCD=YES ; ; PROPERTIES NRTL HENRY-COMPS=HC PROPERTIES SYSOP12 A810 /SYSOP0 A800 / NRTL-HOC ; PROP-SET MASSFLW MASSFLMX UNITS='KG/HR' SUBSTREAM=ALL ; ; Uses the Modified Rackett for Density PROP-REPLACE NRTL NRTL PROP VLMX VLMX49 ; ; Uses Liguid heat capacity equation of DIPPR PROP-REPLACE NRTL NRTL PROP DHL DHL09 ; PROP-DATA VB ; Needed for tray sizing in RADFRAC IN-UNITS SI PROP-LIST VB PVAL GLUCOSE .01850640 PVAL XYLOSE .01850640 PVAL SOLSLDS .01850640 PVAL ARABINOS .01850640 PVAL GALACTOS .01850640 PVAL MANNOSE .01850640 PVAL GLUCOLIG .01850640 PVAL CELLOB .01850640 PVAL XYLOLIG .01850640 PVAL MANOLIG .01850640 PVAL GALAOLIG .01850640 PVAL ARABOLIG .01850640 PVAL XYLITOL .01850640 PVAL LGNSOL .01850640 PVAL EXTRACT .01850640 PVAL PROTEIN .01850640 ; PROP-DATA MULDIP ; Needed for Tray sizing in RADFRAC IN-UNITS MET VOLUME-FLOW='CUM/HR' ENTHALPY-FLO='MMKCAL/HR' & HEAT-TRANS-C='KCAL/HR-SQM-K' PRESSURE=BAR TEMPERATURE=C & VOLUME=CUM DELTA-T=C HEAD=METER MOLE-DENSITY='KMOL/CUM' & MASS-DENSITY='KG/CUM' MOLE-ENTHALP='KCAL/MOL' & MASS-ENTHALP='KCAL/KG' HEAT=MMKCAL MOLE-CONC='MOL/L' & PDROP=BAR PROP-LIST MULDIP PVAL XYLOSE -2267.40 138910.0 320.550 0.0 0.0 323.150 & 418.150 PVAL SOLSLDS -2267.40 138910.0 320.550 0.0 0.0 323.0 & 418.0 PVAL ARABINOS -2267.40 138900.0 320.0 0.0 0.0 323.0 & 418.0 PVAL XYLOLIG -2267.40 138900.0 320.0 0.0 0.0 323.0 418.0 PVAL ARABOLIG -2267.40 138900.0 320.0 0.0 0.0 323.0 418.0 PVAL XYLITOL -2267.40 138900.0 320.0 0.0 0.0 323.0 418.0 PVAL LGNSOL -2267.40 138910.0 320.550 0.0 0.0 323.150 & 418.150 PVAL EXTRACT -2267.40 138910.0 320.550 0.0 0.0 323.0 & 418.0 PVAL PROTEIN -2267.40 138910.0 320.550 0.0 0.0 323.0 & 418.0 ; PROP-DATA DATA1 PROP-LIST MW PVAL HMF 126.11160 PVAL NH4ACET 77.08 PVAL NH4OH 35.05 PVAL GLUCOLIG 162.1424 PVAL CELLOB 342.3001 PVAL XYLOLIG 132.11612 PVAL TAR 150.1314 PVAL MANOLIG 162.1424 PVAL GALAOLIG 162.1424 PVAL ARABOLIG 132.11612 PVAL XYLITOL 152.15 ; PROP-DATA DATA2 IN-UNITS SI ; Use water's dipole moment and radius of gyration, ; these properties are important for the vapor fugacity ; calculation in one block using Hayden & O'Connell. ; These particular components will not be in the vapor ; phase so their values are unimportant. PROP-LIST MUP / RGYR PVAL GLUCOSE 5.84934E-25 / 6.15E-11 PVAL XYLOSE 5.84934E-25 / 6.15E-11 PVAL SOLSLDS 5.84934E-25 / 6.15E-11 PVAL ARABINOS 5.84934E-25 / 6.15E-11 PVAL GALACTOS 5.84934E-25 / 6.15E-11 PVAL MANNOSE 5.84934E-25 / 6.15E-11 PVAL UNKNOWN 5.84934E-25 / 6.15E-11 PVAL GLUCOLIG 5.84934E-25 / 6.15E-11 PVAL CELLOB 5.84934E-25 / 6.15E-11 PVAL XYLOLIG 5.84934E-25 / 6.15E-11 PVAL MANOLIG 5.84934E-25 / 6.15E-11 PVAL GALAOLIG 5.84934E-25 / 6.15E-11 PVAL ARABOLIG 5.84934E-25 / 6.15E-11 PVAL ACETOLIG 5.84934E-25 / 6.15E-11 PVAL XYLITOL 5.84934E-25 / 6.15E-11 PVAL LGNSOL 5.84934E-25 / 6.15E-11 PVAL EXTRACT 5.84934E-25 / 6.15E-11 PVAL PROTEIN 5.84934E-25 / 6.15E-11 ; ;======================================================================= ;/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\ ; LGNSOL -- Soluble Lignin from modified glucose ; Kept TC, PC, VC, TB, OMEGA, RKZTRA, PLXANT, DHVLWT from glucose ; ATOMNO & NOATOM from LIGNIN-1 ; DHFORM same as LIGNIN-1's DHSFRM ; DGFORM assumes difference between DHFORM & DGFORM is the same for ; LGNSOL and glucose ; Heat Capacity (CPIG) calc from LIGNIN ; PROP-DATA IN-UNITS SI PROP-LIST TC / PC / VC / TB / OMEGA / DHFORM / RKTZRA ;/ DGFORM PVAL LGNSOL 1011.1 / 0.62000E+07 / 0.41650 / 825.40 / 2.5674 / -1.96405E+9 / 0.35852 ;/ -1.61648E+09 ; PROP-LIST CPIG PVAL LGNSOL 2.07E5 0.00000 0.00000 & 0.00000 0.00000 0.00000 & 250 1000 0.00000 & 0.00000 0.00000 ; PROP-LIST PLXANT PVAL LGNSOL 1182.2 -84682. 0.00000 & 0.15640 -175.85 -0.23777E-04 & 2.0000 573.15 993.15 ; PROP-LIST DHVLWT PVAL LGNSOL 4.1868E6 298 0.38 & 0.00000 200 ; PROP-LIST ATOMNO PVAL LGNSOL 6 1 8 0 0 0 0 0 0 0 ; PROP-LIST NOATOM PVAL LGNSOL 10 13.9 1.3 0 0 0 0 0 0 0 ;/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/ ; Soluble Solids, Extractives and Protein Info from feedstock analysis PROP-DATA IN-UNITS SI ; Heat of Formation PROP-LIST DHFORM PVAL SOLSLDS 1.340E9 PVAL EXTRACT 1.340E9 PVAL PROTEIN 1.340E9 ;Composition Information PROP-LIST ATOMNO PVAL SOLSLDS 6 1 8 7 16 0 0 0 0 0 PVAL EXTRACT 6 1 8 7 16 0 0 0 0 0 PVAL PROTEIN 6 1 8 7 16 0 0 0 0 0 ; PROP-LIST NOATOM PVAL SOLSLDS 1 0.0230 5.1503 0.3731 0.00267 0 0 0 0 0 PVAL EXTRACT 1 0.0230 5.1503 0.3731 0.00267 0 0 0 0 0 PVAL PROTEIN 1 0.0230 5.1503 0.3731 0.00267 0 0 0 0 0 ;/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/\/ ;======================================================================= ; Henry component parameters (Non-condensible <==> solvent) ; New Parameters for N2 and O2 taken from version 9.2 to improve ; the calculations involving these two components. ;======================================================================= ; PROP-DATA HENRY-1 IN-UNITS MET PRESSURE=BAR TEMPERATURE=C PROP-LIST HENRY BPVAL CH4 ETHANOL -9.792145 307.7800 2.707700 0.0 10.00000 & 30.00000 BPVAL CH4 H2O 212.5741 -10429.00 -29.24200 -1.2910E-3 & 2.310000 55.00000 BPVAL CO2 ETHANOL 89.58308 -5018.800 -11.89100 0.0 & 10.00000 40.00000 BPVAL O2 ETHANOL -30.29763 651.8400 7.021200 -.0149260 & -25.00000 50.00000 BPVAL N2 ETHANOL -1.930195 -22.08200 2.206100 -8.8300E-3 & -60.00000 50.00000 BPVAL CO2 H2O 181.1861 -8982.000 -25.84600 .0121280 & .2000061 74.70000 BPVAL O2 H2O 216.5931 -9622.000 -31.10700 .0121090 & 6.10352E-6 90.00000 BPVAL N2 H2O -21.86243 -2953.500 10.39600 -.0540060 & 6.10352E-6 72.50000 ; ; Using ethanol Henry's for FURFURAL & HMF ; BPVAL N2 FURFURAL -1.943358 -22.08200 2.206100 -8.8300E-3 & 213.1500 323.1500 BPVAL O2 FURFURAL -30.31079 651.8400 7.021200 -.0149260 & 248.1500 323.1500 BPVAL CH4 FURFURAL -9.792145 307.7800 2.707700 0.0 10.00000 & 30.00000 BPVAL CO2 FURFURAL 89.58308 -5018.800 -11.89100 0.0 & 10.00000 40.00000 BPVAL N2 HMF -1.943358 -22.08200 2.206100 -8.8300E-3 & 213.1500 323.1500 BPVAL O2 HMF -30.31079 651.8400 7.021200 -.0149260 & 248.1500 323.1500 BPVAL CH4 HMF -9.792145 307.7800 2.707700 0.0 10.00000 & 30.00000 BPVAL CO2 HMF 89.58308 -5018.800 -11.89100 0.0 & 10.00000 40.00000 ; ;======================================================================== ; NRTL Binary Parameters generated by Aspen Plus Release 9.1-3 ;======================================================================== ; ; Added in W9806C 6/15/98 - "Lit." values from ASPEN 9.2 ; PROP-DATA NRTL-1 IN-UNITS MET VOLUME-FLOW='CUM/HR' ENTHALPY-FLO='MMKCAL/HR' & HEAT-TRANS-C='KCAL/HR-SQM-K' PRESSURE=BAR TEMPERATURE=C & VOLUME=CUM DELTA-T=C HEAD=METER MOLE-DENSITY='KMOL/CUM' & MASS-DENSITY='KG/CUM' MOLE-ENTHALP='KCAL/MOL' & MASS-ENTHALP='KCAL/KG' HEAT=MMKCAL MOLE-CONC='MOL/L' & PDROP=BAR PROP-LIST NRTL BPVAL ETHANOL H2O 0.0 -55.16980 .30310 0.0 0.0 0.0 75.0 100.0 BPVAL H2O ETHANOL 0.0 670.44420 .30310 0.0 0.0 0.0 75.0 100.0 BPVAL ETHANOL FURFURAL 0.0 139.60130 .30 0.0 0.0 0. 75.0 135.0 BPVAL FURFURAL ETHANOL 0.0 425.89810 .30 0.0 0.0 0. 75.0 135.0 BPVAL ETHANOL HMF 0.0 139.60130 .30 0.0 0.0 0.0 75. 135.0 BPVAL HMF ETHANOL 0.0 425.89810 .30 0.0 0.0 0.0 75.0 135.0 BPVAL H2O FURFURAL 0.0 1309.6940 .39580 0.0 0.0 0.0 95. 140.0 BPVAL FURFURAL H2O 0.0 219.89050 .39580 0.0 0.0 0.0 95. 140.0 BPVAL H2O HMF 0.0 1309.6940 .39580 0.0 0.0 0.0 95.0 140.0 BPVAL HMF H2O 0.0 219.89050 .39580 0.0 0.0 0.0 95.0 140.0 BPVAL ETHANOL GLYCEROL 0.0 384.16910 .61450 0.0 0.0 0. 50. 50. BPVAL GLYCEROL ETHANOL 0.0 208.73190 .61450 0.0 0.0 0. 50. 50. BPVAL H2O GLYCEROL -1.25150 272.60750 .30 0.0 0.0 0. 25. 290.0 BPVAL GLYCEROL H2O -.73180 170.91670 .30 0.0 0.0 0. 25.0 290.0 BPVAL ETHANOL CSL -.80090 246.180 .30 0.0 0.0 0.0 24.99 100.0 BPVAL CSL ETHANOL 3.45780 -586.08090 .30 0.0 0.0 0. 24.990 100.0 BPVAL ETHANOL CNUTR -.80090 246.180 .30 0.0 0.0 0. 24.990 100.0 BPVAL CNUTR ETHANOL 3.45780 -586.08090 .30 0. 0. 0. 24.990 100.0 BPVAL H2O NH3 -6.26840 1525.4540 .30 0.0 0.0 0.0 10. 91.50 BPVAL NH3 H2O 9.61210 -3232.8160 .30 0.0 0.0 0.0 10. 91.50 BPVAL FURFURAL CSL -5.87320 2335.0490 .30 0.0 0.0 0. 58.20 161.7 BPVAL CSL FURFURAL 7.10790 -1265.8370 .30 0.0 0.0 0. 58.20 161.7 BPVAL FURFURAL CNUTR -5.87320 2335.0490 .30 0.0 0. 0. 58.20 161.7 BPVAL CNUTR FURFURAL 7.10790 -1265.8370 .30 0.0 0.0 0. 58.20 161.7 BPVAL HMF CSL -5.87320 2335.0490 .30 0.0 0.0 0.0 58.20 161.70 BPVAL CSL HMF 7.10790 -1265.8370 .30 0.0 0.0 0.0 58.20 161.70 BPVAL HMF CNUTR -5.87320 2335.0490 .30 0.0 0.0 0.0 58.20 161.70 BPVAL CNUTR HMF 7.10790 -1265.8370 .30 0.0 0.0 0.0 58.20 161.70 BPVAL GLYCEROL CSL -.73180 170.91670 .30 0.0 0.0 0. 25.0 290.0 BPVAL CSL GLYCEROL -1.25150 272.60750 .30 0.0 0.0 0. 25.0 290.0 BPVAL GLYCEROL CNUTR -.73180 170.91670 .30 0.0 0.0 0. 25.0 290.0 BPVAL CNUTR GLYCEROL -1.25150 272.60750 .30 0.0 0.0 0. 25.0 290.0 BPVAL NH3 CSL 9.61210 -3232.8160 .30 0.0 0.0 0.0 10. 91.50 BPVAL CSL NH3 -6.26840 1525.4540 .30 0.0 0.0 0.0 10. 91.50 BPVAL NH3 CNUTR 9.61210 -3232.8160 .30 0.0 0.0 0.0 10. 91.50 BPVAL CNUTR NH3 -6.26840 1525.4540 .30 0.0 0.0 0.0 10. 91.50 BPVAL ETHANOL OIL 0.0 490.98060 .29880 0.0 0.0 0.0 45. 45.0 BPVAL OIL ETHANOL 0.0 -172.87780 .29880 0.0 0.0 0.0 45. 45.0 ; ;------------------------------------------------------------------- ; RECYCLE/SEQUENCING ;------------------------------------------------------------------- ; ; NEW TEAR LIST BASED ON THOSE PICKED BY ASPEN FOR W9804A TEAR 576 TRACE=10 / 514 TRACE=10 / 521 ; CONVERGENCE CFUGE3SC SECANT SPEC CFUGE3S CONVERGENCE EVAPCNCC SECANT SPEC EVAPCONC CONVERGENCE EV1SZ SECANT SPEC EV1SIZ CONVERGENCE EV2SZ SECANT SPEC EV2SIZ CONVERGENCE TEAR2 BROYDEN TEAR 621 / QBOILER / QH811 / 812 TEAR-VAR FOR-BLOCK=CWDEM VAR-NAME=CWBL1 PARAM MAXIT=500 CONVERGENCE BRNAIR BROYDEN TEAR QH801 SPEC COMBAIR ; SEQUENCE SEQ3 T507-8 STORE PRODMIX TSTORE SEQUENCE SEQ7 LPSTMD M811ISPT ;SEQUENCE SEQ9 IXRGNFLW A202 S221A S221B SEQUENCE SEQ10 S600 H602 NUTMIX CODCALC1 T606 T606FLSH & CODCALC2 AERAIR T608 CODEND SEQUENCE SEQ11 POWER MISCPOW MPOW1 MPOW2 MPOW5 MPOW6 MPOW8 MPOW10 SEQUENCE SEQ12 CFUGE3SC CFUGESLD S505 S505FLSH (RETURN CFUGE3SC) SEQUENCE SEQ13 EVAPCNCC E501LOSS EV1SZ E501L E502V E502LOSS DCOOL2 & (SEQUENCE SEQ12) T530 EV2SZ E502L E503V E503LOSS E503L & (RETURN EV2SZ) (RETURN EV1SZ) (RETURN EVAPCNCC) ; ;---------------------------------------------------------------- ; FLOWSHEETS ;--------------------------------------------------------------- ; FLOWSHEET A100 ;THIS IS THE FLOWSHEET FOR FEED HANDLING. BLOCK C103A IN=102 107 OUT=104A 104D BLOCK C103B IN=104D OUT=104B 102A BLOCK C103C IN=104A 104B OUT=104 BLOCK M104LOSS IN=102A OUT=103 102B BLOCK M104MIX IN=102B 101 OUT=105 BLOCK MPOW1 IN=WC101 WC102 WC104 WC103 WM103 & WM104 WM105 WM107 & WS101 WS102 WS103 & OUT=WMP1 ; FLOWSHEET A200 ;THIS IS THE FLOWSHEET FOR THE PRETREATMENT AREA AND INCLUDES PRETREATMENT ;AND DETOXIFICATION. BLOCK A201 IN=212 211 OUT=214 BLOCK M202MIX IN=105 214 OUT=214A BLOCK M202LO IN=214A 215 OUT=215A QM202LO BLOCK M202HI IN=215A 216 OUT=217 QM202HI BLOCK T203 IN=217 OUT=218 220 BLOCK S205SPT IN=219 OUT=252 253 BLOCK S205A IN=220 OUT=221 225 BLOCK S205MIX IN=225 252 OUT=254 BLOCK S205B IN=254 OUT=255A 256 BLOCK M205 IN=257 OUT=258 WM205 BLOCK M205COOL IN=258 OUT=259 QM205 BLOCK S205FLSH IN=255A 259 OUT=260 255 BLOCK H205 IN=260 OUT=261 262 QH205 BLOCK H200 IN=221 256 OUT=240 QH200 BLOCK T209 IN=240 227 OUT=228 BLOCK T224 IN=233 228 OUT=239 BLOCK S222 IN=239 OUT=229 230 BLOCK C202 IN=255 230 253 OUT=250 BLOCK P224 IN=250 OUT=232 BLOCK H201+A IN=218 OUT=222 QH201 BLOCK H201+B IN=222 QH201B OUT=520A BLOCK H201- IN=502 QH201 OUT=501 QH201B BLOCK H244 IN=520A OUT=520 QH244 BLOCK MPOW2 IN=WM202 WC202 WC225 WC201 WS205 WS221 WS222 OUT=WMP2 ; FLOWSHEET A300 ;THIS FLOWSHEET MODELS THE SACCHARIFICATION AND FERMENTATION PROCESS. BLOCK H301- IN=301 OUT=301A QH301 BLOCK H301+ IN=590 QH301 OUT=591 QH301EX BLOCK T310 IN=301A 312 422 OUT=301B QF300A BLOCK H302 IN=301B OUT=301C QH302 BLOCK SACCHSPT IN=301C OUT=302 303 BLOCK SEEDMIX IN=303 310 310A OUT=303A BLOCK F301-6F IN=303A OUT=303B QF301-6B BLOCK F301-6FL IN=303B OUT=304C 304 BLOCK FERMMIX IN=302 311 311A 304 OUT=304A BLOCK CONTSPLT IN=304A OUT=304F 304G BLOCK F300CONT IN=304G OUT=304H QF300CNT BLOCK F300F IN=304F OUT=304E QF300B BLOCK T306 IN=306 551 OUT=502 BLOCK F300FLSH IN=304E 304H OUT=308 306 ; FLOWSHEET A400 ;THIS FLOWSHEET MODELS THE CELLULASE PRODUCTION AREA. BLOCK BTMSSPLT IN=232 OUT=401 301 BLOCK CLFDSPLT IN=401 OUT=403 410 BLOCK F401-4MX IN=403 430 OUT=431 BLOCK F401-4 IN=423 431 432 434 OUT=432A QF401-4 BLOCK F401-4FL IN=432A OUT=435 433 BLOCK H415 IN=411 OUT=412 QH415 BLOCK T415 IN=412 410 OUT=412A BLOCK F400 IN=412A 433 413 436 416 417 OUT=417A QF400 BLOCK F400FL IN=417A OUT=419 420 ; STREAM 421 SHOULD BE ZERO IN A SEP SACCH/FERM MODE ; AND IS NOT ADDED TO ANY BLOCK IN AREA 300 BLOCK CLSSPLIT IN=420 OUT=421 422 BLOCK T405 IN=415 414 OUT=416 ; FLOWSHEET A500 ;THIS FLOWSHEET MODELS THE DISTILLATION/DEHYDRATION AREA. BLOCK H512- IN=501 OUT=506 QH512 ; BLOCK H512+ IN=518 QH512 OUT=518A ; BLOCK D501 IN=506 OUT=508 510 518 QCD501 QRD501 ;PS506 BLOCK D502 IN=510 521 OUT=511 516 ;PS511 QCD502 QRD502; BLOCK H506- IN=511 OUT=511C QH506 ; BLOCK H506+ IN=596 QH506 OUT=597 QH506EX ; BLOCK T507-8 IN=511C OUT=515A 514 BLOCK H503 IN=515A OUT=517 QH503 BLOCK H507- IN=517 QH507 OUT=521 ; BLOCK H507+ IN=514 OUT=519 QH507 BLOCK H509 IN=519 OUT=515 QH509 ; BLOCK H502 IN=592 QRD502 OUT=593 QH504EX ; BLOCK H501 IN=594 QRD501 OUT=595 QRD501EX ; BLOCK RECTDUP IN=QCD502 OUT=QC502A QC502B BLOCK E501LOSS IN=QC502A QE501A OUT=QE501L QE501B BLOCK E501L IN=518A QE501B OUT=526 525 BLOCK E502V IN=526 OUT=527 QE502A BLOCK E502LOSS IN=QE502A OUT=QE502L QE502B BLOCK E502L IN=580 QE502B OUT=529 528 BLOCK E503V IN=529 OUT=530 QE503A BLOCK E503LOSS IN=QE503A OUT=QE503L QE503B BLOCK E503L IN=528 QE503B OUT=532 531 BLOCK E501MIX IN=527 530 533 OUT=534A ; ADDED SEPARATE MIXER AND SPLITTER SO WE CAN SEE TOTAL CONDENSATE BLOCK E501WW IN=534A 852 OUT=534B 535 BLOCK E501SPT IN=534B OUT=102 211 251 BLOCK H517 IN=532 OUT=533 QH517 ; VENT SCRUBBER BLOCK VNTMIX IN=508 304C 308 OUT=523 BLOCK VNTSCRUB IN=523 524 OUT=550 551 ; ; 524 WATER, 550 VENT, 551 WASTE WATER BLOCK MPOW5 IN=WC501 WS505 OUT=WMP5 ; PNEUMAPRESS UNIT BLOCK DCOOL2 IN=525 OUT=570 QDCOOL2 BLOCK S505 IN=570 OUT=572 571B BLOCK T530 IN=572 OUT=573 580 BLOCK M505 IN=557 OUT=558 WM505 BLOCK M505COOL IN=558 OUT=559 QM505 BLOCK S505FLSH IN=571B 559 OUT=560 571 BLOCK FWMIX IN=516 573 574 OUT=576 BLOCK RWSPLT IN=576 OUT=219 430 411 ; FLOWSHEET A600 ;THIS SECTION MODELS THE WASTEWATER TREATMENT AREA. BLOCK S600 IN=262 520 821 535 944 OUT=612 BLOCK H602 IN=612 OUT=613 QH602 BLOCK NUTMIX IN=613 630 OUT=632 BLOCK T606 IN=632 OUT=613C BLOCK T606FLSH IN=613C OUT=615 618 BLOCK T608 IN=618 626 627 OUT=619A BLOCK T608FLSH IN=619A OUT=620 621 BLOCK T610 IN=621 OUT=625 624 BLOCK S614 IN=625 631 OUT=627 623 BLOCK MPOW6 IN=WC614 WS614 WM604 WM612 WS600 WT610 & OUT=WMP6 ; FLOWSHEET A700 ;THIS FLOWSHEET MODELS THE STORAGE AREA. BLOCK DCOOLE IN=515 OUT=515E BLOCK PRODMIX IN=515E 701 OUT=703 BLOCK TSTORE IN=710 713 717 723 735 745 750 755 OUT=702 ; FLOWSHEET A800 ;THIS FLOWSHEET MODELS THE FUEL AND GAS SIDE OF THE BOILER. BLOCK M803CMB IN=615 803 804B 840 OUT=804C QM803 BLOCK M801MIX IN=571A 623 531 OUT=803 BLOCK M802MIX IN=804 261 560 OUT=804E BLOCK M802 IN=804E OUT=804A WCOMBFAN BLOCK H801- IN=804A QH801 OUT=804B BLOCK M801STM IN=853 OUT=854 QM801 BLOCK M801FLSH IN=571 QM801 OUT=851 571A BLOCK M801CND IN=851 OUT=852 QM801B BLOCK H801+ IN=804D OUT=809A QH801 BLOCK M803HEAT IN=804C QM803 OUT=804D QM803T BLOCK M804 IN=809A OUT=810 809 BLOCK QCOMSPLT IN=QM803T OUT=QCOMLOSS QBOILER ; FLOWSHEET A810 ;THIS FLOWSHEET MODELS THE STEAM SIDE OF THE BOILER/TURBOGENERATOR. BLOCK P826AS IN=813 OUT=813A WP826 BLOCK H811+ IN=813A QH811B OUT=813B QH811 BLOCK M803BD IN=813B QBOILER OUT=813C 821 QSUPER BLOCK M803SHTR IN=813C QSUPER OUT=812 QM803EX BLOCK M811XSPT IN=812 OUT=812C 812D BLOCK M811HTRB IN=812C OUT=812A WM811H BLOCK M811HSPT IN=812A OUT=812B 814 814A BLOCK M811ITRB IN=814A OUT=814B WM811I BLOCK M811ISPT IN=814B OUT=815A 815B 815 BLOCK M811LTRB IN=815B OUT=815C WM811L BLOCK M811LSPT IN=815C OUT=815D 860 BLOCK E501LB IN=860 OUT=861 QE501A2 BLOCK M811VLRB IN=815D OUT=815E WM811VL BLOCK T824AS IN=816A 823 824 OUT=811A BLOCK P824AS IN=811 811A OUT=811B WP824 BLOCK T826 IN=811B 815A OUT=812E 813 QDEAER BLOCK H811-A IN=812B QH811 OUT=819 QH811EX BLOCK H811-B IN=819 OUT=823 QH811B BLOCK M811CND IN=815E OUT=816 QM811 BLOCK P811AS IN=816 OUT=816A WP811 BLOCK M811GEN IN=WM811L WM811I WM811H WM811VL OUT=WLOST WTOTAL BLOCK MPOW8 IN=WM801 WM804 WM830 WM832 WM834 OUT=WMP8 ; FLOWSHEET A900 ;THIS FLOWSHEET MODELS THE MISCELLANEOUS UTILITIES ; Heatcw-s Cooling Water Heat Load accumulator ; HeatCHW- Chilled Water Heat Load accumulator ; BLOCK SSCFCW IN=QF300B QF300CNT OUT=QF300 BLOCK CHCWDUP IN=QH914 OUT=QH914A QH914B QH914C BLOCK SSCFSDCW IN=QF301-6B OUT=QF301 BLOCK QH14BSP IN=QH914B OUT=QH14BCW QH14BCHW BLOCK HEATCW-S IN= QH602 QM811 QM205 QM401 QM505 QH503 QM801B & QH509 QH517 QH200 QCD501 QH415 QH205 QH244 & QF300A QH302 & OUT=QTTOTAL BLOCK QTDUP IN=QTTOTAL OUT=QTTOTA QTTOTB QTTOTC BLOCK QCWMIX IN=QH914A QTTOTA QC502B OUT=QCWCAP BLOCK CWATCAP IN=945 QCWCAP OUT=940 QTTOTXS BLOCK CWDUP IN=QH14BCW OUT=QH14CWA QH14CWB BLOCK CWATOP IN=946 QTTOTB QH14CWA OUT=947 QTTOTXB BLOCK CWFLSH IN=948 QTTOTC QH14CWB OUT=949 QCWFLXS BLOCK CLTWR IN=941 942 944A OUT=941A BLOCK CHEMIX IN=921 922 OUT=923 BLOCK HEATCHW- IN=QF401-4 QF400 OUT=QCHWTOT BLOCK QCHWMIX IN= QCHWTOT QH914C OUT=QCHWCAP BLOCK CHILWAT IN=950 QCHWCAP OUT=951 QCHILXS BLOCK PMPWK IN=WP101 WP102 WP103 WP104 WP105 & WP201 WP224 WP209 WP222 WP239 & WP205 WP211 WP213 & WP300 WP301 WP302 WP306 WP310 & WP400 WP405 WP420 WP401 & WP501 WP504 WP514 WP503 WP505 WP511 & WP512 WP513 WP515 WP530 & WP611 WP602 WP606 WP608 WP610 WP614 WP616 & WP701 WP703 WP704 WP706 WP707 WP708 WP710 WP720 & WP750 WP760 & WP804 WP828 WP830 WP824 WP826 WP811 & WP902 WP912 WP914 & OUT=WPTOTL BLOCK COMPWK IN=WM401 WCOMBFAN OUT=WCMPTOT BLOCK ACOMP IN=440 OUT=441 WM401 BLOCK AFLSH IN=441 OUT=443 QM401 BLOCK ASPLT IN=443 OUT=432 413 BLOCK AGITAT IN=WT224 WT209 WT232 WT205 & WT300 WT301 WT304 WT305 WT306 WT310 & WT400 WT402-3 WT405 WT530 & WT602 WT606 WT608 WT720 WT760 & OUT=WMIX BLOCK WKMIX IN=WPTOTL WCMPTOT WMIX WTOTAL WMISC WM503 & WPLNTPOW WP223 WP755 WC755 OUT=WKNET BLOCK CHCWMIX IN=QF300 QF301 OUT=QWELL BLOCK H914 IN=903 QWELL OUT=904 QH914 BLOCK T914 IN=624 943 251 OUT=905 BLOCK H910 IN=906 OUT=909 QH910 BLOCK CIPCS IN=914 OUT=916 BLOCK MPOW10 IN=WM902 WS904 WM908 OUT=WMP10 BLOCK AIRCMP IN=WM205 WM505 WM904A OUT=WM904 BLOCK MPOWTOT IN=WMP1 WMP2 WMP5 WMP6 WMP8 WMP10 WM910 WM904 & OUT=WMISC BLOCK WKSEP IN=WKNET WTOTAL2 OUT=WPLANT ; ;======================================================================= ; Streams ;======================================================================= ; STREAM 101 ;FEED STREAM ; Basis 2000 dry metric tonnes/day ; Total flow 2,000,000 Kg/day ; 83,333 Kg/hr ; ; Water flow with 52.1% solids = 83333*(1-0.521)/0.521=76615 ; Soluble Solids mass flow = 83333*0.0003 = 25 kg/hr ; CISOLID flow = 83333-25=83308 kg/hr SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW H2O 14706 / SOLSLDS 4342 / EXTRACT 2167 / PROTEIN 3367 SUBSTREAM CISOLID TEMP=20.0 PRES=1.0 MASS-FLOW=73458 MASS-FRAC CELLULOS 0.4203 / XYLAN 0.2260 / ARABINAN 0.0287 / MANNAN 0.0151 / GALACTAN 0.0182 / LIGNIN 0.2061 / ACETATE 0.0268 / ASH 0.0588 ; STREAM 107 ; POLYMER FOR CLARIFIER / BELT PRESS ; CONTROLLED BY POLY1 SUBSTREAM MIXED TEMP=20 PRES=1 MASS-FLOW=5 MASS-FRAC WNUTR 1.0 ; STREAM 211 ;RECYCLE WATER TO PRETREATMENT (A-201) ;CONTROLLED BY RECYCLE SUBSTREAM MIXED TEMP=73.48 PRES=3.0 MASS-FLOW=47243. MASS-FRAC H2O .9910 / FURFURAL 0.0030 / CSL 0.0030 / AACID 0.0030 ; STREAM 212 ;INLET ACID STREAM SUBSTREAM MIXED TEMP=20.0 PRES=3.4022982 MASS-FLOW=500 MASS-FRAC H2SO4 1.0 ; STREAM 215 ;MEDIUM PRESSURE STEAM TO M202LO IN PRETREATMENT ;CONTROLLED BY DESIGN SPEC LPSTMFLO SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 MASS-FLOW H2O 19400.0 ; STREAM 216 ;HIGH PRESSURE STEAM TO RAISE PRETREATMENT REACTOR ;TO REACTION TEMPERATURE ;CONTROLLED BY DESIGN SPEC REACHEAT SUBSTREAM MIXED PRES=13.0 TEMP=268.1893 & MASS-FLOW=42638.0 NPHASE=2 MASS-FLOW H2O 42662.0 ; STREAM 219 ;RECYCLE WATER TO BLOWDOWN TANK ;CONTROLLED BY RECYCLE SUBSTREAM MIXED TEMP=100.0 PRES=1.0 MASS-FLOW=127700. & NPHASE=1 PHASE=L MASS-FRAC H2O .9909 / LACID 0.0055 / AACID 0.0036 SUBSTREAM CISOLID TEMP=100.0 PRES=1.0 MASS-FLOW=327 MASS-FRAC ZYMO .34 / LIGNIN .33 / CELLULAS .33 ; STREAM 227 ;LIME FOR OVERLIMING ;Controlled by Fortran OLIME SUBSTREAM CISOLID TEMP=20.0 PRES=1.0 MASS-FLOW=987.30 NPHASE=1 & PHASE=S MASS-FRAC CAH2O2 1.0 ; STREAM 233 ;H2SO4 FOR REACIDIFYING ;Controlled by Fortran REACID SUBSTREAM MIXED TEMP=20.0 PRES=3.4022982 MASS-FLOW=421.0 MASS-FRAC H2SO4 1.0 ; STREAM 257 SUBSTREAM MIXED TEMP=25. PRES=1. & MOLE-FLOW=2360. MASS-FRAC N2 0.79 / O2 0.21 ; STREAM 310 SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW DAP 500 ; STREAM 311 SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW DAP 500 ; STREAM 310A SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW CSL 850.0 ; STREAM 311A SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW CSL 5116. ; STREAM 312 ; Cellulase to saccharification T310 SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW H2O 9167 SUBSTREAM CISOLID TEMP=20.0 PRES=1.0 MASS-FLOW CELLULAS 833 ; STREAM 411 ;RECYCLE WATER STREAM TO CELLULASE FERMENTORS ;CONTROLLED BY RECYCLE SUBSTREAM MIXED TEMP=100.0 PRES=1.0 NPHASE=1 PHASE=L & MASS-FLOW=22703 MASS-FRAC H2O 1.0 ;.9565 / SOLSLDS .008 / ; XYLOSE .0052 / LACID 0.0194 / AACID 0.0109 SUBSTREAM CISOLID TEMP=100.0 PRES=1.0 & MASS-FLOW=58. MASS-FRAC LIGNIN 0.34 / CELLULAS 0.33 / ZYMO 0.33 ; STREAM 414 ;CSL FOR CELLULASE PRODUCTION ;CONTROLLED BY FORTRAN CSL-ENZY SUBSTREAM MIXED TEMP=20. PRES=1.0 MASS-FLOW CSL 463 ; STREAM 415 ;NUTRIENT STREAM FOR CELLULASE PRODUCTION ;CONTROLLED BY FORTRAN CSL-ENZY SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW CNUTR 200 ; STREAM 417 ;ANTI-FOAM STREAM FOR CALCULATING STORAGE TANK ;CONTROLLED BY FORTRAN CSL-ENZY SUBSTREAM MIXED TEMP=20. PRES=1. MASS-FLOW OIL 238. ; STREAM 423 ;CSL FOR CELLULASE SEED PRODUCTION ;CONTROLLED BY FORTRAN CSL-ENZY SUBSTREAM MIXED TEMP=20. PRES=1.0 MASS-FLOW CSL 30.5 ; STREAM 430 ;RECYCLE STREAM FOR CELLULASE SEED PRODUCTION ;CONTROLLED BY RECYCLE SUBSTREAM MIXED TEMP=100.0 PRES=1.0 MASS-FLOW=2143. & NPHASE=1 PHASE=L MASS-FRAC H2O .9838 / XYLOSE .0052/ SOLSLDS .011 SUBSTREAM CISOLID TEMP=100.0 PRES=1.0 MASS-FLOW=5.5 MASS-FRAC CELLULOS .015 / LIGNIN .07 / BIOMASS 8.44E-5/ GYPSUM 0.915 ; STREAM 432A ;TEAR STREAM INITIAL GUESS SUBSTREAM MIXED TEMP=28.0 PRES=1.0 MASS-FLOW H2O 2871. / N2 16652. / CO2 146. / O2 4324. / CSL 34. SUBSTREAM CISOLID TEMP=28.0 PRES=1.0 MASS-FLOW LIGNIN 62. / BIOMASS 48. ; STREAM 434 SUBSTREAM MIXED TEMP=28.0 PRES=1.0 MASS-FLOW=16. MASS-FRAC NH3 .5 / SO2 .5 ; STREAM 436 SUBSTREAM MIXED TEMP=28.0 PRES=1.0 MASS-FLOW=162.0 MASS-FRAC NH3 .5 / SO2 .5 ; STREAM 501 SUBSTREAM MIXED TEMP=30.0 PRES=1.0 MASS-FLOW=380640. MASS-FRAC ETHANOL .04 / H2O .9587 / OIL 0.0013 SUBSTREAM CISOLID TEMP=30.0 PRES=1.0 MASS-FLOW=31667. MASS-FRAC CELLULOS 0.18 / LIGNIN 0.82 ; STREAM 508 ;TEAR STREAM INITIAL GUESS SUBSTREAM MIXED TEMP=33.8 PRES=1.81 MASS-FLOW ETHANOL 70 / H2O 23 / CO2 483 ; STREAM 514 SUBSTREAM MIXED TEMP=116 VFRAC=1.0 MASS-FLOW ETHANOL 18474. / H2O 92. ; STREAM 521 ; Initial guess for recycle from Mole-sieve SUBSTREAM MIXED TEMP=50 PRES=1 MASS-FLOW=6428 MASS-FRAC ETHANOL 0.7 / H2O 0.3 ; STREAM 524 ; Well water for vent scrubber SUBSTREAM MIXED TEMP=26 PRES=1 MASS-FLOW H2O 1000 ; STREAM 557 SUBSTREAM MIXED TEMP=25. PRES=1. & MOLE-FLOW=2870. MASS-FRAC N2 0.79 / O2 0.21 ; STREAM 574 ;FRESH MAKE-UP WATER ADDED TO RECYCLE WATER SUBSTREAM MIXED TEMP=20 PRES=1.0 MASS-FLOW H2O 211205. ; STREAM 576 ;iNITIAL GUESS SUBSTREAM MIXED TEMP=51 PRES=1.0 MASS-FLOW H2O 148270 ; STREAM 590 ;THIS IS THE STEAM REQ'D TO HEAT THE HYDROLYZATE ;FOR SACCHARIFICATION IN H301. ;CONTROLLED BY DESIGN-SPEC SACCHHEAT SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 MASS-FLOW H2O 7700. ; STREAM 592 ;THIS IS THE STEAM REQ'D TO TRIM THE REBOILER ;FOR THE RECTIFICATION COLUMN ;CONTROLLED BY DESIGN-SPEC TRIM SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 MASS-FLOW H2O 6303. ; STREAM 594 ;THIS IS THE STEAM REQ'D TO RUN THE BEER COLUMN ;REBOILER. ;CONTROLLED BY DESIGN-SPEC REBOIL SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 MASS-FLOW H2O 50000. ; STREAM 596 ;STEAM TO SUPERHEAT ETHANOL TO MOLE SIEVE ;CONTROLLED BY DESIGN SPEC SUPRHET SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 MASS-FLOW H2O 298.1 ; STREAM 621 ;INITIAL GUESS SUBSTREAM MIXED TEMP=21 PRES=1.0 MASS-FLOW=168610 MASS-FRAC H2O 0.9985 / CSL 0.0015 SUBSTREAM CISOLID TEMP=21 PRES=1.0 MASS-FLOW=86. MASS-FRAC BIOMASS 1.0 ; STREAM 626 ;OXYGEN FOR AEROBIC TREATMENT ;CONTROLLED BY FORTRAN AERAIR SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW=6944.0 MASS-FRAC O2 0.21 / N2 0.79 ; STREAM 630 ;WASTEWATER TREATMENT NUTRIENTS ;CONTROLLED BY FORTRAN WWNUTR SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW WNUTR 171. ; STREAM 631 ; POLYMER FOR BELT PRESS ; CONTROLLED BY WWNUTR2 SUBSTREAM MIXED TEMP=20 PRES=1 MASS-FLOW=5 MASS-FRAC WNUTR 1.0 ; STREAM 701 ;DENATURANT FOR FINAL BLENDING ;CONTROLLED BY FORTRAN STORE SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW=812. MASS-FRAC DENAT 1.0 ; STREAM 710 ;H2SO4 STREAM FOR CALCULATING STORAGE TANK ;CONTROLLED BY FORTRAN STORE SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW=514. MASS-FRAC H2SO4 1.0 ; STREAM 713 ;FIREWATER STREAM FOR CALCULATING STORAGE TANK SUBSTREAM MIXED TEMP=20 PRES=1.0 MASS-FLOW=6271. MASS-FRAC H2O 1.0 ; STREAM 717 ;AMMONIA STREAM FOR CALCULATING STORAGE TANK ;CONTROLLED BY FORTRAN STORE SUBSTREAM MIXED TEMP=20. PRES=17 MASS-FLOW=229.6 MASS-FRAC NH3 1.0 ; STREAM 723 ;DIESEL FUEL STREAM FOR CALCULATING STORAGE TANK ;CONTROLLED BY FORTRAN STORE SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW=14.97 MASS-FRAC PROPANE 1.0 ; STREAM 735 ;TOTAL CSL STREAM FOR CELLULASE & ETHANOL PRODUCTION ;CONTROLLED BY FORTRAN CSL-ENZY SUBSTREAM MIXED TEMP=20. PRES=1.0 MASS-FLOW CSL 1138.4 ; STREAM 745 ;TOTAL LIME ;CONTROLLED BY PHCONTR1 SUBSTREAM CISOLID TEMP=20.0 PRES=1.0 MASS-FLOW CAH2O2 1.0 ; STREAM 750 ; Cellulase SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW H2O 9167 SUBSTREAM CISOLID TEMP=20.0 PRES=1.0 MASS-FLOW CELLULAS 833 ; STREAM 755 ; Diammonium Phosphate (DAP), SSCF nutrient SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW DAP 1000.0 STREAM 804 ;INLET AIR STREAM TO THE COMBUSTION FAN (M802) ;CONTROLLED BY DESIGN-SPEC COMBAIR ; AIR COMPOSITION FROM FOSTER WHEELER IN REI 1998 SUBCONTRACT ;Using the following molar composition of dry air (78.084% N2, 20.946% O2, ;0.033% CO2, & 0.934% Ar from CRC 63rd ed. p.F-171) and an air molecular ;weight of 28.964 (CRC 63rd ed.) dry air is 23.14% O2 on a mass basis. ;Assuming that all non-oxygen components can be modeled as N2, dry air is ;76.86% (mass) N2. Then assuming that water causes equal dissipation of ;all components a stream that is 1.3% (mass) water is 22.84% O2 and ;75.86% N2. SUBSTREAM MIXED TEMP=75 PRES=1.0 MASS-FLOW=255240.0 MASS-FRAC H2O .0130 / N2 .7586 / O2 .2284 ; STREAM 811 ;BFW MAKE-UP SUBSTREAM MIXED TEMP=26.0 PRES=3.4 MASS-FLOW H2O 73157.1 ; STREAM 812 ; Tear stream initial guess SUBSTREAM MIXED TEMP=510.0 PRES=86.0577 MASS-FLOW H2O 206560 ; STREAM 814 ;HP (150 PSIG)PROCESS STEAM TO PRETREATMENT AND DISTILLATION ;CONTROLLED BY FORTRAN BLOCK HPSTMD SUBSTREAM MIXED PRES=13.0 VFRAC=1.0 MASS-FLOW=85575.7 & NPHASE=2 MASS-FLOW H2O 85575.7 ; STREAM 815 ;LP (50 PSIG) PROCESS STEAM TO PRETREATMENT AND HEATERS ;CONTROLLED BY FORTRAN BLOCK LPSTMD SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 & MASS-FLOW=55203.2 MASS-FRAC H2O 1.0 ; STREAM 815A ;LP STEAM TO DEAERATOR ;CONTROLLED BY DESIGN-SPEC DEAERHT SUBSTREAM MIXED TEMP=163.5110 PRES=4.42290 MASS-FLOW H2O 38054.8 ; STREAM 821 ;INITIAL GUESS SUBSTREAM MIXED TEMP=321 PRES=112 MASS-FLOW H2O 7219.0 ; STREAM 824 ;CONDENSATE MAKE-UP SUBSTREAM MIXED PRES=1.7 VFRAC=.0 MASS-FLOW H2O 120622. ; STREAM 840 ;Auxillary fuel to supplement burner/boiler SUBSTREAM MIXED TEMP=25 PRES=1.0 MASS-FLOW CH4 .00001 ; For biomass use same definition as for stream 101 ; MASS-FLOW H2O 73530 / SOLSLDS 23375 / EXTRACT 13835 / PROTEIN 16835 ; SUBSTREAM CISOLID TEMP=20.0 PRES=1.0 MASS-FLOW=362625 ; MASS-FRAC CELLULOS 0.4285 / XYLAN 0.2361 / ; ARABINAN 0.0255 / MANNAN 0.0018 / ; GALACTAN 0.0139 / LIGNIN 0.2015 / ; ACETATE 0.0225 / ASH 0.0701 ; STREAM 853 ;HIGH PRESSURE STEAM FOR LIGNIN DRYER ;PER ReTec QUOTE NEEDS TO BE AT LEAST 160 PSI SATURATED STEAM ;CONTROLLED BY DESIGN SPEC LPSTMFLO SUBSTREAM MIXED TEMP=268.1895 PRES=13.0 MASS-FLOW H2O 0.0000001 ; STREAM 903 ;PROCESS MAKE-UP WATER DEMAND ;CONTROLLED BY FORTRAN BLOCK WATERDEM SUBSTREAM MIXED TEMP=13 PRES=1.0 MASS-FLOW H2O 100000.0 ; STREAM 906 ;CIP/CS WATER SUBSTREAM MIXED TEMP=20. PRES=1.0 MASS-FLOW H2O 63.04 ; STREAM 914 SUBSTREAM MIXED TEMP=20. PRES=1.0 MASS-FLOW H2O 63.04 ; STREAM 921 SUBSTREAM MIXED PRES=1.0 TEMP=20.0 MASS-FLOW H2O 3 ; STREAM 922 SUBSTREAM MIXED PRES=1.0 TEMP=20 MASS-FLOW H2O 4 ; STREAM 440 SUBSTREAM MIXED TEMP=20.0 PRES=1.0 MASS-FLOW=126347. MASS-FRAC N2 .790 / O2 .210 ; STREAM 441 SUBSTREAM MIXED TEMP=152.6 PRES=2.7 MASS-FLOW=323200. MASS-FRAC N2 .790 / O2 .210 ; STREAM 944 ; Specified Cooling Tower Blowdown SUBSTREAM MIXED TEMP=28. PRES=1.0 MASS-FLOW H2O 17820 ; STREAM 941 ; Place holder for Calculated Cooling Twr Make-up SUBSTREAM MIXED TEMP=28. PRES=1.0 MASS-FLOW H2O 30682.0 ; STREAM 942 ; Place holder for calculated Cooling Tower Windage SUBSTREAM MIXED TEMP=28. PRES=1.0 MASS-FLOW H2O 30682.0 ; STREAM 943 ; Place holder for Well water Mixed with treated water SUBSTREAM MIXED TEMP=26. PRES=1.0 MASS-FLOW H2O 30682.0 ; STREAM 944A ; Place Holder for calculated Cooling Tower Blowdown ; Used as a comparison to the actual specified as 944 ; above. SUBSTREAM MIXED TEMP=28. PRES=1.0 MASS-FLOW H2O 30682.0 ; STREAM 945 SUBSTREAM MIXED TEMP=28. PRES=4.0827578 MASS-FLOW H2O 100.0 ; STREAM 946 SUBSTREAM MIXED TEMP=28. PRES=4.0827578 MASS-FLOW H2O 100.0 ; STREAM 948 SUBSTREAM MIXED TEMP=28. PRES=1. MASS-FLOW H2O 100000.0 ; STREAM 950 SUBSTREAM MIXED TEMP=4.0 PRES=4.0827578 MASS-FLOW H2O .3e7 ; ;--------------------------------------------------------------------- ; HEAT STREAMS ;------------------------------------------------------------------- ; ; QCD502 and QRD502 are the condenser and reboiler duties to column ; AS-502. They will be determined by the FORTRAN D502QCR. ; Updated 3/22/02 by KI ; STREAM QCD501 INFO HEAT DUTY=.1126 ; STREAM QRD501 INFO HEAT DUTY=-32.335 ; STREAM QCD502 INFO HEAT DUTY=20.4354 ; STREAM QRD502 INFO HEAT DUTY=-3.8248 ; STREAM QH602 ; TEAR -- INITIAL GUESS INFO HEAT DUTY=8555900 ; STREAM QH801 ; TEAR -- INITIAL GUESS INFO HEAT DUTY=.765 ; STREAM QBOILER ; TEAR -- INITIAL GUESS INFO HEAT DUTY=133.184 ; STREAM QH811 ; TEAR -- INITIAL GUESS INFO HEAT DUTY=-6.0634 ; STREAM QH14CWB ; TEAR -- INITIAL GUESS INFO HEAT DUTY=8.3025 ; STREAM QE501A INFO HEAT DUTY=0.0000001 ; DEF-STREAMS HEAT QH201B QH205 QH244 & QCD502 QH415 QCD501 QBOILER QF400 & QCHILXS QCHWTOT QF401-4 QM803 QCOMLOSS & QM803T QM811 QDEAER & QH811 QH811EX & QM202LO QM202HI QRD501 QRD501EX & QF301 QH602 QF300A QSUPER & QM803EX QH504EX QRD502 & QH503 QH201 QH507 QH301 QH302 & QH910 QTTOTAL QTTOTXS QH506 QH301EX & QH506EX QH509 QM505 QH512 QF301-6B & QF300B QF300 QF300CNT QH200 & QM205 QM401 QWELL QH914 & QH914A QH914B QH914C QTTOTA QTTOTB & QTTOTXB QH14BCW QH14BCHW QE501L QE501B & QE502A QE502L QE502B QE503A QE503L & QE503B QH517 QH14CWA QH14CWB QTTOTC & QCWFLXS QDCOOL2 QCWCAP QCHWCAP QM801 & QC502A QC502B QH801 QE501A QE501A2 & QM801B QH811B ; ;---------------------------------------------------------------------- ; WORK STREAMS ;---------------------------------------------------------------------- ; DEF-STREAMS WORK WM401 WP826 WCMPTOT WCOMBFAN & WP824 WM811H WM811I WKNET WLOST & WM811L WMISC WMIX WM503 WM910 & WP201 WP224 WP239 WP209 WP222 WP300 WP301 WP302 WP310 & WP400 WP405 WP420 WP501 WP504 WP514 WP515 WP530 WP611 & WP602 WP606 WP608 WP610 WP614 WP616 WM604 WM612 & WS600 WT610 WP701 & WP703 WP704 WP706 WP707 WP708 WP710 WP720 WP804 WP828 & WP750 WP902 WP912 WP914 & WP503 WP505 WP101 WP102 WP103 WP104 WP105 WP830 & WPLNTPOW WP511 WP512 WP513 WP223 WP306 WP401 & WM811VL WM205 WM505 WP205 WP211 WP213 WP755 WC755 WP760 ; WM503 is Mole Sieve Power Requirement STREAM WM503 INFO WORK POWER=250 ; ;THE FOLLOWING WPP STREAMS ARE PUMP & Compressor WORK STREAMS ; DEF-STREAMS WORK WP811 WPTOTL WTOTAL ; ;THE FOLLOWING WT STREAMS ARE AGITATOR WORK STREAMS ; Agitator streams are controlled by FORTRAN POWER unless otherwise noted ; DEF-STREAMS WORK WT224 WT209 WT232 WT205 WT300 WT310 & WT301 WT304 WT305 WT306 WT400 & WT402-3 WT606 WT608 WT405 & WT602 WT530 WT720 WT760 ; ;WT608 is Anaerobic Digestor agitation ;Calculated by CODCALC2 STREAM WT608 INFO WORK POWER=10 ; ; WT224 is Reacidification Tank Agitator Power (A-224) STREAM WT224 INFO WORK POWER=10 ; ; WT209 is Overliming Tank Agitator Power (A-209) STREAM WT209 INFO WORK POWER=10 ; ; WT232 is Slurrying Tank Agitator Power (A-232) STREAM WT232 INFO WORK POWER=10 ; ; WT205 is Hydrolysate Mix Tank Agitator Power (A-205) STREAM WT205 INFO WORK POWER=10 ; ; WT300 is Fermenter Agitator Power (GA-300A-W) STREAM WT300 INFO WORK POWER=10 ; ; WT301 is Zymo Seed Hold Tank Agitator Power (A-301A/B) STREAM WT301 INFO WORK POWER=10 ; ; WT310 is Saccharification Agitator Power (GA-310A-W) STREAM WT300 INFO WORK POWER=10 ; ; WT400 is Cellulase Production Agitator Power (A-401A-L) STREAM WT400 INFO WORK POWER=10 ; ; WT402-3 is Cellulase Seed Production Fermenter Power (A-402-4A/B) STREAM WT402-3 INFO WORK POWER=10 ; ; WT530 is Recycled Water Ag. Power (A-530) STREAM WT530 INFO WORK POWER=10 ; ; WT602 is Equalization Basin Agitator Power (A-602) STREAM WT602 INFO WORK POWER=10 ; ; WT606 is Anaerobic Digesters Power (A-606) ; Controlled by CODCALC1 STREAM WT606 INFO WORK POWER=10 ; ; WT720 is CSL Storage Tank Agitator Power (A-720) STREAM WT720 INFO WORK POWER=10 ; The following are miscellaneous work streams. ; DEF-STREAMS WORK WM104 WM105 WM107 WC102 WC104 WC103 WM103 & WMP1 & WC101 WS101 WS102 WS103 & WM202 WC201 WS205 WC202 WS221 WS222 WC225 & WMP2 WTOTAL2 WPLANT & WC501 WS505 WMP5 WC614 WS614 WMP6 & WM801 WM804 WM830 WM832 WM834 WMP8 & WM902 WM904 WM904A WS904 WM908 WMP10 ; ;---------- Area 100 Miscellaneous Work Streams Wood Chips STREAM WM104 INFO WORK POWER=0 ; WM104 is disk refiner power (M-104) ; Controlled by FORTRAN MISCPOW STREAM WC102 INFO WORK POWER=0 ; WC102 is radial stacker power (C-101) ; Controlled by FORTRAN MISCPOW STREAM WC104 INFO WORK POWER=0 ; WC104 is unknown conveyor power (C-103) ; Controlled by FORTRAN MISCPOW STREAM WC103 INFO WORK POWER=0 ; WC103 is milled chip conveyor power (C-104) ; Controlled by FORTRAN MISCPOW STREAM WM103 INFO WORK POWER=0 ; WM103 is magnetic chip cleaner power (M-103) ; Controlled by FORTRAN MISCPOW ; STREAM WS103 INFO WORK POWER=0 ; WS103 is tramp iron magnet power (S-103) ; Set at 0.0 because power is unknown and assumed to be low (like R0008B) ; Not modified by fortrans ; ; Miscellaneous Work Streams - Area 150 Sawdust STREAM WMP1 INFO WORK POWER=0 ; WMP1 is the summary miscellaneous work stream for Area 1000 ; and is calculated in MPOW1 ; ;----- Area 200 Miscellaneous Work Streams STREAM WM202 INFO WORK POWER=0 ; WM202 is the prehydrolysis screw feeder power (M-202) ; Controlled by FORTRAN MISCPOW STREAM WC201 INFO WORK POWER=0 ; WC201 is flash tank screw conveyor power (C-201) ; Controlled by FORTRAN MISCPOW STREAM WS205 INFO WORK POWER=0 ; WS205 is the hydrolysate filter press power (S-202) ; Controlled by FORTRAN MISCPOW STREAM WC202 INFO WORK POWER=0 ; WC202 is cake washing conveyor power (C-202) ; Controlled by FORTRAN MISCPOW STREAM WS221 INFO WORK POWER=0 ; WS221 is the ISEP unit power (S-221) ; Controlled by FORTRAN MISCPOW STREAM WC225 INFO WORK POWER=0 ; WC225 is lime solids feeder power (C-225) ; Controlled by FORTRAN MISCPOW STREAM WMP2 INFO WORK POWER=0 ; WMP2 is the miscellaneous work summary stream for Area 2000 and is ; calculated in MPOW2 ; ; --------- Area 500 Miscellaneous Work Streams ; STREAM WC501 INFO WORK POWER=0 ; WC501 is the sludge screw power (C-501) ; Controlled by FORTRAN MISCPOW ; STREAM WS505 INFO WORK POWER=0 ; WS505 is the pneumapress power (S-505) ; Controlled by FORTRAN MISCPOW ; STREAM WMP5 INFO WORK POWER=0 ; WMP5 is the miscellaneous summary work stream for Area 5000 and is ; calculated in MPOW5 ; ; --------- Area 600 Miscellaneous Work Streams ; STREAM WC614 INFO WORK POWER=0 ; WC614 is the digestion cell mass screw power (C-614) ; Controlled by FORTRAN MISCPOW STREAM WS614 INFO WORK POWER=0 ; WS614 is the finishing belt filter press power (S-614) ; Controlled by FORTRAN MISCPOW STREAM WMP6 INFO WORK POWER=0 ; WMP6 is the miscellaneous summary work stream for Area 6000 and is ; calculated in MPOW6 ; ; --------- Area 800 Miscellaneous Work Streams ; STREAM WM804 INFO WORK POWER=0 ; WM804 is the combustion gas baghouse power (M-804) ; Controlled by FORTRAN MISCPOW STREAM WM830 INFO WORK POWER=0 ; WM830 is the hydrazine addition package power (M-830) ; Controlled by FORTRAN MISCPOW STREAM WM832 INFO WORK POWER=0 ; WM832 is the ammonia addition package power (M-832) ; Controlled by FORTRAN MISCPOW STREAM WM834 INFO WORK POWER=0 ; WM834 is the phosphate addition package power (M-832) ; Controlled by FORTRAN MISCPOW STREAM WMP8 INFO WORK POWER=0 ; WMP8 is the miscellaneous summary work stream for Area 8000 and ; is calculated in MPOW8 ; ; ; --------- Area 900 Miscellaneous Work Streams ; STREAM WM902 INFO WORK POWER=0 ; WM902 is the cooling tower package power (M-902) ; Controlled by FORTRAN MISCPOW STREAM WM904 INFO WORK POWER=0 ; WM904 is the sum air compressor power requirement (M-904) ; Controlled by FORTRAN MISCPOW STREAM WM904A INFO WORK POWER=0 ; WM904A is the plant and instrument air compressor power (M-904) ; Controlled by FORTRAN MISCPOW STREAM WS904 INFO WORK POWER=0 ; WS904 is the instrument air dryer power (S-904) ; Controlled by FORTRAN MISCPOW STREAM WM908 INFO WORK POWER=0 ; WM908 is the chilled water system power (M-908) ; Controlled by FORTRAN MISCPOW STREAM WMP10 INFO WORK POWER=0 ;WMP10 is the miscellaneous work summary stream for Area 900 and is ;calculated in MPOW10 ; ;------------------------------------------------------------ ; BLOCK SECTION ; SOLIDS HANDLING BLOCKS - AREA 100 ;------------------------------------------------------------ ; BLOCK C103A SEP DESCRIPTION "CLARIFIER POLYMER REMOVAL" PARAM PRES=1.0 FRAC STREAM=104A SUBSTREAM=MIXED COMPS= & H2O ETHANOL FURFURAL HMF H2SO4 N2 CO2 O2 CH4 & NO NO2 NH3 SOLSLDS GLUCOSE XYLOSE GALACTOS & MANNOSE ARABINOS UNKNOWN AACID LACID CNUTR WNUTR & CSL OIL DENAT GLUCOLIG CELLOB XYLOLIG MANOLIG & GALAOLIG ARABOLIG ACETOLIG GLYCEROL SUCCACID & XYLITOL LGNSOL EXTRACT PROTEIN & FRACS=.0 .0 .0 .0 .0 .0 .0 .0 .0 & .0 .0 .0 .0 .0 .0 .0 & .0 .0 .0 .0 .0 .0 1.0 & .0 .0 .0 .0 .0 .0 .0 & .0 .0 .0 .0 .0 & .0 .0 .0 .0 ;ALL CNUTR & CSL SHOULD HAVE BEEN CONSUMED IN CELLULASE PRODUCTION & ;SO ANY REMAINING SHOULD GO OFF TO WWT SO THAT THE RECYCLE WILL BE ;CORRECT. DENAT AND WNUTR SHOULD NOT BE IN THIS STREAM, BUT IF THEY ;ARE, THEY BEHAVE LIKE ANY LIQUID. FRAC STREAM=104A SUBSTREAM=CISOLID COMPS=CELLULOS XYLAN & ARABINAN MANNAN GALACTAN LIGNIN BIOMASS CELLULAS & ZYMO CASO4 CAH2O2 GYPSUM TAR ACETATE ASH & FRACS= .0 .0 & .0 .0 .0 .0 .0 .0 & .0 0.0 0.0 0.0 .0 .0 0.0 ; BLOCK C103B FSPLIT DESCRIPTION "RECYCLED MAKE-UP WATER AND LOSS WITH DIRT SPLITTER" ; Set by RECCOND MASS-FLOW 104B 1000.0 ; BLOCK C103C MIXER DESCRIPTION "MIXES POLYMER AND WATER FOR WASTE REMOVAL" ; BLOCK M104LOSS FSPLIT DESCRIPTION "MAKE-UP WATER AND EVAPORATION/WINDAGE LOSS SPLITTER" ; Set by RECCOND MASS-FLOW 103 11300.0 ; BLOCK M104MIX MIXER DESCRIPTION "MIXES INCOMING BIOMASS WITH RETAINED WASH WATER" ; BLOCK MPOW1 MIXER DESCRIPTION "AREA 1000 MISCELLANEOUS WORK SUMMER" ; ; ;------------------------------------------------------------ ; ; PRETREATMENT BLOCKS - AREA 200 ;------------------------------------------------------------ ; BLOCK A201 MIXER DESCRIPTION "INLINE SULFURIC ACID MIXER" PARAM PRES=4.0 ; BLOCK M202MIX MIXER DESCRIPTION "IMPREGNATOR - DESIGNED TO HEAT MIX TO 100 C" PARAM PRES=.0 ; BLOCK M202LO HEATER DESCRIPTION "HEATER TO GET FLUIDS TO RXN TEMP" PARAM TEMP=100 PRES=39.26 ; BLOCK T203 FLASH2 DESCRIPTION "PREHYDROLYSIS BLOWDOWN TANK" PROPERTIES NRTL-HOC PARAM PRES=1.0 DUTY=.0 ; BLOCK H200 HEATER DESCRIPTION "HYDROLYSATE SLURRY COOLER" PARAM TEMP=50. PRES=.0 ; BLOCK C202 MIXER DESCRIPTION "MIX CENTRIFUGE LIQUID STREAMS" PARAM PRES=.0 ; BLOCK P224 MIXER DESCRIPTION "MIX DETOXED SLURRY AND RECYCLE WATER" ; BLOCK S205SPT FSPLIT DESCRIPTION "RECYCLE WATER SPLITTER" ; Calculated in FORTRAN S205WASH MASS-FLOW 252 125000.0 ; BLOCK H244 HEATER DESCRIPTION "COOL BLOWDOWN VAPOR PRIOR TO WWT" PARAM PRES=0.0 TEMP=30.0 ; BLOCK S205A SSPLIT DESCRIPTION "PRE-WASH SEPARATIONS FOR S-202" PROPERTIES NRTL-HOC PARAM PRES=.0 FRAC MIXED 225 0.145 FRAC CISOLID 225 0.995 ; THE MIXED FRACTION IS CALCULATED BY DESIGN-SPEC CT-S205A ; BLOCK S205MIX MIXER DESCRIPTION "MIXES WASH-WATER WITH SINGLE-PRESSED SOLIDS" PARAM PRES=.0 ; BLOCK S205B SEP DESCRIPTION "POST-WASH SEPARATIONS FOR S205" PARAM PRES=.0 ;THE FRACTIONAL SPLITS ARE BASED ON HARRIS 2000 SUBCONTRACT ;PNEUMAPRESS TEST 9. 93.3% OF THE TOTAL INLET SOLUBLES ARE ;RECOVERED TO FILTRATE. 99.5% OF INSOLUBLE SOLIDS ARE RECOVERED ;TO CAKE FRAC STREAM=256 SUBSTREAM=MIXED COMPS= & H2O ETHANOL FURFURAL HMF H2SO4 N2 CO2 O2 CH4 & NO NO2 NH3 SOLSLDS GLUCOSE XYLOSE GALACTOS & MANNOSE ARABINOS UNKNOWN AACID LACID CNUTR WNUTR & CSL OIL DENAT GLUCOLIG CELLOB XYLOLIG MANOLIG & GALAOLIG ARABOLIG ACETOLIG GLYCEROL SUCCACID & XYLITOL LGNSOL EXTRACT PROTEIN & FRACS=.75 .9 .9 .9 .9 .9 .9 .9 .9 & .9 .9 .9 .9 0.9 .9 .9 & .9 .9 .9 .9 .9 0.9 .9 & .9 .9 .9 .9 .9 .9 .9 & .9 .9 .9 .9 .9 & .9 .9 .9 .9 ;ACCORDING TO HARRIS MEETING 17 Jan 01 99.5% OF INSOLUBLE SOLIDS ;ARE RECOVERED BY THE PNEUMAPRESS FRAC STREAM=255A SUBSTREAM=CISOLID COMPS=CELLULOS XYLAN & ARABINAN MANNAN GALACTAN LIGNIN BIOMASS CELLULAS & ZYMO CASO4 CAH2O2 GYPSUM TAR ACETATE ASH & FRACS= 1.0 1.0 & 1.0 1.0 1.0 1.0 1.0 1.0 & 1.0 1.0 1.0 1.0 1.0 1.0 1.0 ; BLOCK M205 COMPR DESCRIPTION "AIR COMPRESSOR FOR PNEUMAPRESS SYSTEM" PARAM TYPE=ISENTROPIC DELP=125. SEFF=0.72 ; BLOCK M205COOL HEATER DESCRIPTION "COOLER FOR COMPRESSED PNEUMAPRESS AIR" ; PARAM PRES=1.0 TEMP=40.0 PARAM TEMP=40.0 ; BLOCK S205FLSH FLASH2 DESCRIPTION "AIR-SOLID CONTACT IN PNEUMAPRESS" PARAM PRES=.0 DUTY=.0 ; BLOCK H205 FLASH2 DESCRIPTION "CONDENSER ON PNEUMAPRESS VENT" PARAM TEMP=38.0 PRES=.0 ; BLOCK S222 SSPLIT DESCRIPTION "GYPSUM REMOVAL S/L SEP" FRAC MIXED 229 0.004 FRAC CISOLID 229 0.995 ; BLOCK T224 RSTOIC DESCRIPTION "REACIDIFICATION TANK" PARAM PRES=.0 STOIC 1 MIXED H2SO4 -1.0 / CISOLID CAH2O2 -1.0 / GYPSUM 1.0 CONV 1 CISOLID CAH2O2 1.0 ; BLOCK M202HI RSTOIC DESCRIPTION "PREHYDROLYSIS (SUNDS) REACTOR" PARAM TEMP=190 VFRAC=0.0 SERIES=NO STOIC 1 CISOLID CELLULOS -1.0 / MIXED GLUCOLIG 1.0 STOIC 2 MIXED H2O -1.0 / CISOLID CELLULOS -2.0 / MIXED CELLOB 1.0 STOIC 3 MIXED H2O -1.0 / CISOLID CELLULOS -1.0 / MIXED GLUCOSE 1.0 STOIC 4 CISOLID CELLULOS -1.0 / MIXED HMF 1.0 / MIXED H2O 2.0 STOIC 5 CISOLID XYLAN -1.0 / MIXED XYLOLIG 1.0 STOIC 6 MIXED H2O -1.0 / CISOLID XYLAN -1.0 / MIXED XYLOSE 1.0 STOIC 7 CISOLID XYLAN -1.0 / MIXED FURFURAL 1.0 / MIXED H2O 2.0 STOIC 8 MIXED H2O -1.0 / CISOLID XYLAN -1.0 / CISOLID TAR 1.0 STOIC 9 CISOLID MANNAN -1.0 / MIXED MANOLIG 1.0 STOIC 10 MIXED H2O -1.0 / CISOLID MANNAN -1.0 / MIXED MANNOSE 1.0 STOIC 11 CISOLID MANNAN -1.0 / MIXED HMF 1.0 / MIXED H2O 2.0 STOIC 12 CISOLID GALACTAN -1.0 / MIXED GALAOLIG 1.0 STOIC 13 MIXED H2O -1.0 / CISOLID GALACTAN -1.0 / MIXED GALACTOS 1.0 STOIC 14 CISOLID GALACTAN -1.0 / MIXED HMF 1.0 / MIXED H2O 2.0 STOIC 15 CISOLID ARABINAN -1.0 / MIXED ARABOLIG 1.0 STOIC 16 MIXED H2O -1.0 / CISOLID ARABINAN -1.0 / MIXED ARABINOS 1.0 STOIC 17 CISOLID ARABINAN -1.0 / MIXED H2O 2.0 / MIXED FURFURAL 1.0 STOIC 18 MIXED H2O -1.0 / CISOLID ARABINAN -1.0 / CISOLID TAR 1.0 STOIC 19 CISOLID ACETATE -1.0 / MIXED ACETOLIG 1.0 STOIC 20 CISOLID ACETATE -1.0 / MIXED AACID 1.0 STOIC 21 MIXED H2O -3.0 / MIXED FURFURAL -1.0 / CISOLID TAR 1.0 STOIC 22 MIXED H2O -3.0 / MIXED HMF -1.0 / CISOLID TAR 1.2 STOIC 23 CISOLID LIGNIN -1.0 / MIXED LGNSOL 1.0 ; CONV 1 CISOLID CELLULOS 0.007 CONV 2 CISOLID CELLULOS 0.007 CONV 3 CISOLID CELLULOS 0.070 CONV 4 CISOLID CELLULOS 0.0 CONV 5 CISOLID XYLAN 0.025 CONV 6 CISOLID XYLAN 0.90 CONV 7 CISOLID XYLAN 0.05 CONV 8 CISOLID XYLAN 0.0 CONV 9 CISOLID MANNAN 0.025 CONV 10 CISOLID MANNAN 0.90 CONV 11 CISOLID MANNAN 0.05 CONV 12 CISOLID GALACTAN 0.025 CONV 13 CISOLID GALACTAN 0.90 CONV 14 CISOLID GALACTAN 0.05 CONV 15 CISOLID ARABINAN 0.025 CONV 16 CISOLID ARABINAN 0.90 CONV 17 CISOLID ARABINAN 0.05 CONV 18 CISOLID ARABINAN 0.0 CONV 19 CISOLID ACETATE 0.0 CONV 20 CISOLID ACETATE 1.0 CONV 21 MIXED FURFURAL 1.0 CONV 22 MIXED HMF 1.0 CONV 23 CISOLID LIGNIN 0.05 ; BLOCK T209 RSTOIC DESCRIPTION "OVERLIMING TANK T-209" PARAM PRES=.0 TEMP=50. NPHASE=1 PHASE=L STOIC 1 MIXED H2SO4 -1.0 / CISOLID CAH2O2 -1.0 / GYPSUM 1.0 CONV 1 MIXED H2SO4 1.0 ; BLOCK MPOW2 MIXER DESCRIPTION "AREA 2000 MISCELLANEOUS WORK SUMMER" ; ;------------------------------------------------------------ ; SACCHARIFICATION AND CO-FERMENTATION BLOCKS - AREA 300 ;------------------------------------------------------------ ; BLOCK SACCHSPT FSPLIT DESCRIPTION "FEED SPLITTER TO SEED TRAIN" FRAC 303 0.1 ; ;10% IS SAME VALUE IN SSFSPLT IN SSF MODEL ;SOURCE NOT DOCUMENTED ; BLOCK FERMMIX MIXER DESCRIPTION "MIX CSL, DAP AND SEED WITH HYD. BEFORE FERM" ; BLOCK CONTSPLT FSPLIT DESCRIPTION "SPLIT TO CONTAMINATION REACTION" FRAC 304G 0.03 ;3% Contamination ; BLOCK T306 MIXER DESCRIPTION "BEER WELL" ; BLOCK F300FLSH FLASH2 DESCRIPTION "DUMMY BLOCK TO RELEASE GASES FROM FERM" PARAM PRES=1.0 DUTY=0.0 ; BLOCK H301- HEATER DESCRIPTION "HYDROLYSATE SLURRY HEATER FOR SACCH." PARAM TEMP=65. PRES=.0 ; BLOCK H301+ HEATER DESCRIPTION "STEAM SIDE OF HYDROLYSATE SLURRY HEATER" PARAM PRES=0.0 VFRAC=0.0 ; BLOCK T310 RSTOIC DESCRIPTION "SSCF FERMENTORS HYDROLYSIS BLOCK" PARAM TEMP=65.0 PRES=1.0 SERIES=NO ; THE HYDROLYSIS REACTIONS ARE CALCULATED IN THIS BLOCK. ; THE REACTIONS NEEDED FOR FERMENTATION HAVE BEEN COMMENTED OUT. STOIC 1 CISOLID CELLULOS -1.0 / MIXED GLUCOLIG 1.0 STOIC 2 CISOLID CELLULOS -2.0 / MIXED H2O -1.0 / MIXED CELLOB 1.0 STOIC 3 CISOLID CELLULOS -1.0 / MIXED H2O -1.0 / MIXED GLUCOSE 1.0 STOIC 4 MIXED GLUCOLIG -2.0 / MIXED H2O -1.0 / MIXED CELLOB 1.0 STOIC 5 MIXED GLUCOLIG -1.0 / MIXED H2O -1.0 / MIXED GLUCOSE 1.0 STOIC 6 MIXED CELLOB -1.0 / MIXED H2O -1.0 / MIXED GLUCOSE 2.0 STOIC 13 CISOLID XYLAN -1.0 / MIXED XYLOLIG 1.0 STOIC 14 CISOLID XYLAN -1.0 / MIXED H2O -1.0 / MIXED XYLOSE 1.0 STOIC 15 MIXED XYLOLIG -1.0 / MIXED H2O -1.0 / MIXED XYLOSE 1.0 STOIC 23 CISOLID ARABINAN -1.0 / MIXED ARABOLIG 1.0 STOIC 24 CISOLID ARABINAN -1.0 / MIXED H2O -1.0 / MIXED ARABINOS 1.0 STOIC 25 MIXED ARABOLIG -1.0 / MIXED H2O -1.0 / MIXED ARABINOS 1.0 STOIC 32 CISOLID GALACTAN -1.0 / MIXED GALAOLIG 1.0 STOIC 33 CISOLID GALACTAN -1.0 / MIXED H2O -1.0 / MIXED GALACTOS 1.0 STOIC 34 MIXED GALAOLIG -1.0 / MIXED H2O -1.0 / MIXED GALACTOS 1.0 STOIC 41 CISOLID MANNAN -1.0 / MIXED MANOLIG 1.0 STOIC 42 CISOLID MANNAN -1.0 / MIXED H2O -1.0 / MIXED MANNOSE 1.0 STOIC 43 MIXED MANOLIG -1.0 / MIXED H2O -1.0 / MIXED MANNOSE 1.0 ; ; THE CONVERSTIONS TO ETHANOL ARE BASED ON PD 23 #3 MODIFIED ; SO THAT 4% OF MONOMERIC SUGARS ARE CONVERTED TO CELL MASS ; CONV 1 CISOLID CELLULOS 0.04 CONV 2 CISOLID CELLULOS 0.012 CONV 3 CISOLID CELLULOS 0.9 CONV 4 MIXED GLUCOLIG 0.0 CONV 5 MIXED GLUCOLIG 0.0 CONV 6 MIXED CELLOB 1.0 CONV 13 CISOLID XYLAN 0.0 CONV 14 CISOLID XYLAN 0.0 CONV 15 MIXED XYLOLIG 0.0 CONV 23 CISOLID ARABINAN 0.0 CONV 24 CISOLID ARABINAN 0.0 CONV 25 MIXED ARABOLIG 0.0 CONV 32 CISOLID GALACTAN 0.0 CONV 33 CISOLID GALACTAN 0.0 CONV 34 MIXED GALAOLIG 0.0 CONV 41 CISOLID MANNAN 0.0 CONV 42 CISOLID MANNAN 0.0 CONV 43 MIXED MANOLIG 0.0 ; BLOCK F300F RSTOIC DESCRIPTION "FERMENTORS FERMENTATION BLOCK" PARAM TEMP=41.0 PRES=1.0 SERIES=NO ; THE FERMENTATION REACTIONS ARE CALCULATED IN THIS BLOCK ; THE HYDROLYSIS REACTIONS HAVE BEEN COMMENTED OUT STOIC 7 MIXED GLUCOSE -1.0 / ETHANOL 2.0 / CO2 2.0 STOIC 8 MIXED GLUCOSE -1.0 / CSL -1.0 / DAP -0.018 / CISOLID ZYMO 6.0 / MIXED H2O 2.4 / MIXED O2 0.3 STOIC 9 MIXED GLUCOSE -1.0 / H2O -2.0 / MIXED GLYCEROL 2.0 / O2 1.0 STOIC 10 MIXED GLUCOSE -1.0 / CO2 -2.0 / MIXED SUCCACID 2.0 / O2 1.0 STOIC 11 MIXED GLUCOSE -1.0 / AACID 3.0 STOIC 12 MIXED GLUCOSE -1.0 / LACID 2.0 STOIC 16 MIXED XYLOSE -3.0 / ETHANOL 5.0 / CO2 5.0 STOIC 17 MIXED XYLOSE -1.0 / CSL -0.835 / DAP -0.015 / CISOLID ZYMO 5.0 / MIXED H2O 2.0 / MIXED O2 0.25 STOIC 18 MIXED XYLOSE -3.0 / H2O -5.0 / MIXED GLYCEROL 5.0 / O2 2.5 STOIC 19 MIXED XYLOSE -1.0 / H2O -1.0 / MIXED XYLITOL 1.0 / O2 0.5 STOIC 20 MIXED XYLOSE -3.0 / CO2 -5.0 / MIXED SUCCACID 5.0 / O2 2.5 STOIC 21 MIXED XYLOSE -2.0 / AACID 5.0 STOIC 22 MIXED XYLOSE -3.0 / LACID 5.0 STOIC 26 MIXED ARABINOS -3.0 / ETHANOL 5.0 / CO2 5.0 STOIC 27 MIXED ARABINOS -1.0 / CSL -0.835 / DAP -0.015 / CISOLID ZYMO 5.0 / MIXED H2O 2.0 / MIXED O2 0.25 STOIC 28 MIXED ARABINOS -3.0 / H2O -5.0 / MIXED GLYCEROL 5.0 / O2 2.5 STOIC 29 MIXED ARABINOS -3.0 / CO2 -5.0 / MIXED SUCCACID 5.0 / O2 2.5 STOIC 30 MIXED ARABINOS -2.0 / AACID 5.0 STOIC 31 MIXED ARABINOS -3.0 / LACID 5.0 STOIC 35 MIXED GALACTOS -1.0 / ETHANOL 2.0 / CO2 2.0 STOIC 36 MIXED GALACTOS -1.0 / CSL -1.0 / DAP -0.018 / CISOLID ZYMO 6.0 / MIXED H2O 2.4 / MIXED O2 0.3 STOIC 37 MIXED GALACTOS -1.0 / H2O -2.0 / MIXED GLYCEROL 2.0 / O2 1.0 STOIC 38 MIXED GALACTOS -1.0 / CO2 -2.0 / MIXED SUCCACID 2.0 / O2 1.0 STOIC 39 MIXED GALACTOS -1.0 / AACID 3.0 STOIC 40 MIXED GALACTOS -1.0 / LACID 2.0 STOIC 44 MIXED MANNOSE -1.0 / ETHANOL 2.0 / CO2 2.0 STOIC 45 MIXED MANNOSE -1.0 / CSL -1.0 / DAP -0.018 / CISOLID ZYMO 6.0 / MIXED H2O 2.4 / MIXED O2 0.3 STOIC 46 MIXED MANNOSE -1.0 / H2O -2.0 / MIXED GLYCEROL 2.0 / O2 1.0 STOIC 47 MIXED MANNOSE -1.0 / CO2 -2.0 / MIXED SUCCACID 2.0 / O2 1.0 STOIC 48 MIXED MANNOSE -1.0 / AACID 3.0 STOIC 49 MIXED MANNOSE -1.0 / LACID 2.0 ; CONV 7 MIXED GLUCOSE 0.95 CONV 8 MIXED GLUCOSE 0.02 CONV 9 MIXED GLUCOSE 0.004 CONV 10 MIXED GLUCOSE 0.006 CONV 11 MIXED GLUCOSE 0.015 CONV 12 MIXED GLUCOSE 0.002 CONV 16 MIXED XYLOSE 0.85 CONV 17 MIXED XYLOSE 0.019 CONV 18 MIXED XYLOSE 0.003 CONV 19 MIXED XYLOSE 0.046 CONV 20 MIXED XYLOSE 0.009 CONV 21 MIXED XYLOSE 0.014 CONV 22 MIXED XYLOSE 0.002 CONV 26 MIXED ARABINOS 0.85 CONV 27 MIXED ARABINOS 0.019 CONV 28 MIXED ARABINOS 0.003 CONV 29 MIXED ARABINOS 0.015 CONV 30 MIXED ARABINOS 0.014 CONV 31 MIXED ARABINOS 0.002 CONV 35 MIXED GALACTOS 0.85 CONV 36 MIXED GALACTOS 0.019 CONV 37 MIXED GALACTOS 0.003 CONV 38 MIXED GALACTOS 0.015 CONV 39 MIXED GALACTOS 0.014 CONV 40 MIXED GALACTOS 0.002 CONV 44 MIXED MANNOSE 0.85 CONV 45 MIXED MANNOSE 0.019 CONV 46 MIXED MANNOSE 0.003 CONV 47 MIXED MANNOSE 0.015 CONV 48 MIXED MANNOSE 0.014 CONV 49 MIXED MANNOSE 0.002 ; BLOCK F300CONT RSTOIC DESCRIPTION "FERMENTORS CONTAMINATION BLOCK" PARAM TEMP=41.0 PRES=1.0 SERIES=NO ; ALL FERMENTABLE SUGARS ARE CONVERTED TO LACTIC ACID IN THIS BLOCK ; THE FRACTION OF SUGAR LOST TO CONTAMINATION IS SET IN CONTSPLT STOIC 1 MIXED GLUCOSE -1.0 / LACID 2.0 STOIC 2 MIXED XYLOSE -3.0 / LACID 5.0 STOIC 3 MIXED ARABINOS -3.0 / LACID 5.0 STOIC 4 MIXED GALACTOS -1.0 / LACID 2.0 STOIC 5 MIXED MANNOSE -1.0 / LACID 2.0 CONV 1 MIXED GLUCOSE 1.0 CONV 2 MIXED XYLOSE 1.0 CONV 3 MIXED ARABINOS 1.0 CONV 4 MIXED GALACTOS 1.0 CONV 5 MIXED MANNOSE 1.0 ; BLOCK H302 HEATER DESCRIPTION "SACCHARIFIED SLURRY COOLER BEFORE FERMENTATION" PARAM TEMP=41. PRES=.0 ; BLOCK SEEDMIX MIXER DESCRIPTION "MIX CSL AND DAP WITH HYD BEFORE SEED FERM" ; BLOCK F301-6F RSTOIC DESCRIPTION "SSCF SEED FERMENTORS FERMENTATION" PARAM TEMP=41.0 PRES=1.0 SERIES=NO ; THE FERMENTATION REACTIONS ARE CALCULATED IN THIS BLOCK ; THE HYDROLYSIS REACTIONS HAVE BEEN COMMENTED OUT STOIC 7 MIXED GLUCOSE -1.0 / ETHANOL 2.0 / CO2 2.0 STOIC 8 MIXED GLUCOSE -1.0 / CSL -1.0 / DAP -0.018 / CISOLID ZYMO 6.0 / MIXED H2O 2.4 / MIXED O2 0.3 STOIC 9 MIXED GLUCOSE -1.0 / H2O -2.0 / MIXED GLYCEROL 2.0 / O2 1.0 STOIC 10 MIXED GLUCOSE -1.0 / CO2 -2.0 / MIXED SUCCACID 2.0 / O2 1.0 STOIC 11 MIXED GLUCOSE -1.0 / AACID 3.0 STOIC 12 MIXED GLUCOSE -1.0 / LACID 2.0 STOIC 16 MIXED XYLOSE -3.0 / ETHANOL 5.0 / CO2 5.0 STOIC 17 MIXED XYLOSE -1.0 / CSL -0.835 / DAP -0.015 / CISOLID ZYMO 5.0 / MIXED H2O 2.0 / MIXED O2 0.25 STOIC 18 MIXED XYLOSE -3.0 / H2O -5.0 / MIXED GLYCEROL 5.0 / O2 2.5 STOIC 19 MIXED XYLOSE -1.0 / H2O -1.0 / MIXED XYLITOL 1.0 / O2 0.5 STOIC 20 MIXED XYLOSE -3.0 / CO2 -5.0 / MIXED SUCCACID 5.0 / O2 2.5 STOIC 21 MIXED XYLOSE -2.0 / AACID 5.0 STOIC 22 MIXED XYLOSE -3.0 / LACID 5.0 STOIC 26 MIXED ARABINOS -3.0 / ETHANOL 5.0 / CO2 5.0 STOIC 27 MIXED ARABINOS -1.0 / CSL -0.835 / DAP -0.015 / CISOLID ZYMO 5.0 / MIXED H2O 2.0 / MIXED O2 0.25 STOIC 28 MIXED ARABINOS -3.0 / H2O -5.0 / MIXED GLYCEROL 5.0 / O2 2.5 STOIC 29 MIXED ARABINOS -3.0 / CO2 -5.0 / MIXED SUCCACID 5.0 / O2 2.5 STOIC 30 MIXED ARABINOS -2.0 / AACID 5.0 STOIC 31 MIXED ARABINOS -3.0 / LACID 5.0 STOIC 35 MIXED GALACTOS -1.0 / ETHANOL 2.0 / CO2 2.0 STOIC 36 MIXED GALACTOS -1.0 / CSL -1.0 / DAP -0.018 / CISOLID ZYMO 6.0 / MIXED H2O 2.4 / MIXED O2 0.3 STOIC 37 MIXED GALACTOS -1.0 / H2O -2.0 / MIXED GLYCEROL 2.0 / O2 1.0 STOIC 38 MIXED GALACTOS -1.0 / CO2 -2.0 / MIXED SUCCACID 2.0 / O2 1.0 STOIC 39 MIXED GALACTOS -1.0 / AACID 3.0 STOIC 40 MIXED GALACTOS -1.0 / LACID 2.0 STOIC 44 MIXED MANNOSE -1.0 / ETHANOL 2.0 / CO2 2.0 STOIC 45 MIXED MANNOSE -1.0 / CSL -1.0 / DAP -0.018 / CISOLID ZYMO 6.0 / MIXED H2O 2.4 / MIXED O2 0.3 STOIC 46 MIXED MANNOSE -1.0 / H2O -2.0 / MIXED GLYCEROL 2.0 / O2 1.0 STOIC 47 MIXED MANNOSE -1.0 / CO2 -2.0 / MIXED SUCCACID 2.0 / O2 1.0 STOIC 48 MIXED MANNOSE -1.0 / AACID 3.0 STOIC 49 MIXED MANNOSE -1.0 / LACID 2.0 ; ; THE CONVERSTIONS TO ETHANOL ARE BASED ON EPD0005 RUN ; MODIFIED SO THAT 4% OF MONOMERIC SUGARS ARE CONVERTED ; TO CELL MASS AND ALL SUGARS ARE CONSUMED. ; CONV 7 MIXED GLUCOSE 0.90 CONV 8 MIXED GLUCOSE 0.04 CONV 9 MIXED GLUCOSE 0.004 CONV 10 MIXED GLUCOSE 0.006 CONV 11 MIXED GLUCOSE 0.015 CONV 12 MIXED GLUCOSE 0.002 CONV 16 MIXED XYLOSE 0.8 CONV 17 MIXED XYLOSE 0.04 CONV 18 MIXED XYLOSE 0.003 CONV 19 MIXED XYLOSE 0.046 CONV 20 MIXED XYLOSE 0.009 CONV 21 MIXED XYLOSE 0.014 CONV 22 MIXED XYLOSE 0.002 CONV 26 MIXED ARABINOS 0.8 CONV 27 MIXED ARABINOS 0.04 CONV 28 MIXED ARABINOS 0.003 CONV 29 MIXED ARABINOS 0.015 CONV 30 MIXED ARABINOS 0.014 CONV 31 MIXED ARABINOS 0.002 CONV 35 MIXED GALACTOS 0.8 CONV 36 MIXED GALACTOS 0.04 CONV 37 MIXED GALACTOS 0.003 CONV 38 MIXED GALACTOS 0.015 CONV 39 MIXED GALACTOS 0.014 CONV 40 MIXED GALACTOS 0.002 CONV 44 MIXED MANNOSE 0.8 CONV 45 MIXED MANNOSE 0.04 CONV 46 MIXED MANNOSE 0.003 CONV 47 MIXED MANNOSE 0.015 CONV 48 MIXED MANNOSE 0.014 CONV 49 MIXED MANNOSE 0.002 ; BLOCK F301-6FL FLASH2 DESCRIPTION "SEED CO2 VENT" PARAM PRES=1.0 DUTY=0.0 ; ;----------------------------------------------------------- ; CELLULASE BLOCKS - AREA 400 ;---------------------------------------------------------- ; BLOCK T415 MIXER DESCRIPTION "MIXER FOR FEED AND WATER TO CELLULASE PRODUCTION." ; BLOCK F401-4MX MIXER DESCRIPTION & "MIXER FOR FEED AND WATER TO CELLULASE SEED FERMENTORS." ; BLOCK T405 MIXER DESCRIPTION "CELLULASE MEDIA PREP TANK" ; BLOCK BTMSSPLT FSPLIT DESCRIPTION & "SPLIT CENTRIFUGE BOTTOMS BETWEEN CELLULASE FERM & ETOH FERM" FRAC 401 .0220 ;THE FRACTION SPECIFIED IS A GUESS BASED ON THE 1990 BASE CASE. THE ;ACTUAL SPLIT IS CALCULATED BY THE FORTRAN BLOCK ENZYME DEPENDING ON ;THE LOADING REQUIRED IN SSCF. ; BLOCK CLFDSPLT FSPLIT DESCRIPTION "SPLIT BETWEEN SEED AND FERMENTORS." PARAM NPHASE=1 PHASE=L FRAC 403 0.05 ;The following fractionation and note were left by Vicki, I have ignored ;her advice. MR 2 July 97 ; FRAC 403 .005 ;THE FRACTION SPECIFIED WAS SELECTED TO GET A 5% INOCULUM. ;CURRENTLY, IT IS NOT CHANGEABLE DUE TO CHANGING CONDITIONS. ;A CONTROL BLOCK SHOULD BE WRITTEN TO CHANGE THIS. ; BLOCK CLSSPLIT FSPLIT DESCRIPTION & "SPLIT CELL. RCTR EFF. BTWN SEED FERM + ETOH FRM" FRAC 421 .20 ; BLOCK H415 HEATER DESCRIPTION "COOLER FOR CELLULASE PRODUCTION FERMENTOR WATER" PARAM TEMP=40.0 PRES=1.0 ; BLOCK F401-4FL FLASH2 DESCRIPTION "CELLULASE SEED DUMMY FOR FLASH CALC." PARAM PRES=1.0 DUTY=.0 ; BLOCK F400FL FLASH2 DESCRIPTION "CELLULASE PRODUCTION DUMMY FOR FLASH CALC." PARAM PRES=.0 DUTY=.0 ; BLOCK F400 RSTOIC ; SO2 and NH3 addition through stream 436 are set by FORTRAN ; Block NUTRA. If the conversions are changed, FORTRAN must also ; be modified. DESCRIPTION "CELLULASE FERMENTOR" PARAM TEMP=28.0 PRES=1.6603215 STOIC 1 MIXED GLUCOSE -2.0 / O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 9.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 4 MIXED MANNOSE -2.0 / O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 9.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 3 MIXED GALACTOS -2.0 / O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 9.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 2 MIXED XYLOSE -2.0 / O2 -5.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 5.65217 / CISOLID BIOMASS 4.34783 STOIC 5 MIXED ARABINOS -2.0 / O2 -5.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 5.65217 / CISOLID BIOMASS 4.34783 STOIC 6 MIXED GLUCOSE -2.0 / O2 -8.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 10.79310 / CO2 8.55172 / CISOLID CELLULAS 3.44828 STOIC 7 MIXED MANNOSE -2.0 / O2 -8.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 10.79310 / CO2 8.55172 / CISOLID CELLULAS 3.44828 STOIC 8 MIXED GALACTOS -2.0 / O2 -8.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 10.79310 / CO2 8.55172 / CISOLID CELLULAS 3.44828 STOIC 9 MIXED XYLOSE -2.0 / O2 -6.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 8.79310 / CO2 6.55172 / CISOLID CELLULAS 3.44828 STOIC 10 MIXED ARABINOS -2.0 / O2 -6.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 8.79310 / CO2 6.55172 / CISOLID CELLULAS 3.44828 STOIC 11 CISOLID CELLULOS -2.0 / MIXED O2 -8.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 8.79310 / CO2 8.55172 / CISOLID CELLULAS 3.44828 STOIC 12 CISOLID MANNAN -2.0 / MIXED O2 -8.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 8.79310 / CO2 8.55172 / CISOLID CELLULAS 3.44828 STOIC 13 CISOLID GALACTAN -2.0 / MIXED O2 -8.45862 / NH3 -1.0 / SO2 -0.02414 / H2O 8.79310 / CO2 8.55172 / CISOLID CELLULAS 3.44828 ;CONVERSIONS ARE BASED ON THE 1990 BASE CASE. CONV 1 MIXED GLUCOSE 0.470 CONV 2 MIXED XYLOSE 0.470 CONV 3 MIXED GALACTOS 0.470 CONV 4 MIXED MANNOSE 0.470 CONV 5 MIXED ARABINOS 0.470 CONV 6 MIXED GLUCOSE 0.530 CONV 7 MIXED MANNOSE 0.530 CONV 8 MIXED GALACTOS 0.530 CONV 9 MIXED XYLOSE 0.530 CONV 10 MIXED ARABINOS 0.530 CONV 11 CISOLID CELLULOS 1.0 CONV 12 CISOLID MANNAN 1.0 CONV 13 CISOLID GALACTAN 1.0 ; BLOCK F401-4 RSTOIC ; SO2 and NH3 addition through stream 434 is set by FORTRAN ; block NUTRB. If conversions are changed, the FORTRAN must ; also be modified. DESCRIPTION "CELLULASE SEED FERMENTOR" PARAM TEMP=28.0 PRES=1.0 STOIC 1 MIXED GLUCOSE -2.0 / O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 9.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 2 MIXED MANNOSE -2.0 / O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 9.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 3 MIXED GALACTOS -2.0 / O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 9.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 4 MIXED XYLOSE -2.0 / O2 -5.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 5.65217 / CISOLID BIOMASS 4.34783 STOIC 5 MIXED ARABINOS -2.0 / O2 -5.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 5.65217 / CISOLID BIOMASS 4.34783 STOIC 6 CISOLID CELLULOSE -2.0 / MIXED O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 7 CISOLID MANNAN -2.0 / MIXED O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 STOIC 8 CISOLID GALACTAN -2.0 / MIXED O2 -7.45217 / SO2 -0.01522 / NH3 -1. / H2O 7.93478 / CO2 7.65217 / CISOLID BIOMASS 4.34783 ; CONVERSIONS ARE BASED ON THE 1990 BASE CASE. CONV 1 MIXED GLUCOSE 1.0 CONV 2 MIXED MANNOSE 1.0 CONV 3 MIXED GALACTOS 1.0 CONV 4 MIXED XYLOSE 1.0 CONV 5 MIXED ARABINOS 1.0 CONV 6 CISOLID CELLULOS 1.0 CONV 7 CISOLID MANNAN 1.0 CONV 8 CISOLID GALACTAN 1.0 ; ; ;------------------------------------------------------------- ; DISTILLATION BLOCKS - AREA 500 ;------------------------------------------------------------- ; BLOCK H201+A HEATER DESCRIPTION "FEED CROSS EXCHANGER (HOT SIDE)-SENSIBLE" PARAM PRES=.0 VFRAC=1.0 ; BLOCK H201+B HEATER DESCRIPTION "FEED CROSS EXCHANGER (HOT SIDE)-LATENT" PARAM PRES=.0 VFRAC=0.0 ; BLOCK H201- HEATER DESCRIPTION "FEED CROSS EXCHANGER (COLD SIDE)" ;Temp spec causes a problem when flash vapor is at 5 atm (hot wash) ;because only a certain amount of ;heat is available from QH201 and QH201B. Spec P only for hot wash. PARAM TEMP=95.0 PRES=4.0 ; PARAM PRES=4.0 ; BLOCK H512- HEATER DESCRIPTION "BEER COLUMN BTMS/FEED INTERCHANGER, FEED SIDE" PARAM TEMP=100 PRES=70 ; BLOCK H512+ HEATER DESCRIPTION "BEED COL BTMS/FEED INTERCHANGER, BTMS SIDE" PARAM PRES=0 ; BLOCK D501 RADFRAC IN-UNITS ENG PARAM NSTAGE=16 ALGORITHM=NONIDEAL MAXOL=100 SOLID-BAL=STAGE FEEDS 506 2 PRODUCTS 518 16 L / 508 1 V / 510 3 V & MASS-FLOW=105000 PRODUCTS QCD501 1 / QRD501 16 P-SPEC 1 27.4 COL-SPECS DP-COL=3.0 MOLE-RDV=1 MASS-D=1050 MOLE-RR=3 & DP-COND=0.5 T-EST 1 140 / 2 235 / 5 239 / 7 243 / 9 246 / 11 & 248 / 13 252 SPEC 1 TEMP 140 1 STAGE=1 SPEC 2 MASS-FRAC .0005 STAGE=16 COMPS=ETHANOL ; SPEC 3 MASS-FRAC .845 PHASE=V STAGE=1 COMPS=CO2 ; VARY 1 MOLE-RR 1 10 VARY 2 MASS-VPROD 60000 120000 STAGE=3 VARY 3 MASS-D 800 1100 TRAY-SIZE 1 2 15 SIEVE SIZE-DATA COND=YES REB=YES ; ;BLOCK D501 SEP ;; 506 Feed ;; 508 Vent ;; 510 Vapor Draw ;; 518 Bottoms ;; ;; VENT ; FRAC STREAM=508 SUBSTREAM=MIXED COMPS= & ; ETHANOL H2O CO2 N2 O2 & ; FRACS= 0.0032665 0.000065447 1 1 1 ;; ;; BOTTOMS ; FRAC STREAM=518 SUBSTREAM=MIXED COMPS= & ; ETHANOL H2O & ; GLUCOSE XYLOSE SOLSLDS ARABINOS GALACTOS MANNOSE & ; CELLOB XYLOLIG MANOLIG GALAOLIG ARABOLIG XYLITOL & ; H2SO4 GLYCEROL SUCCACID OIL GLUCOLIG & ; AACID FURFURAL HMF NH3 CSL CNUTR LACID & ; & ; FRACS= 0.0079086 .90235 & ; 1 1 1 1 1 1 & ; 1 1 1 1 1 1 & ; 1 1 1 1 1 & ; .95138 .48404 .48404 .002594 .9019 .9019 .99943 ;; ; FRAC STREAM=518 SUBSTREAM=CISOLID COMPS= & ; CELLULOS XYLAN LIGNIN CELLULAS BIOMASS ZYMO GYPSUM ASH & ; TAR ARABINAN MANNAN & ; FRACS=1 1 1 1 1 1 1 1 & ; 1 1 1 ; FLASH-SPECS 508 TEMP=140 PRES=26.6 ; FLASH-SPECS 510 TEMP =113.75 VFRAC=1 ; FLASH-SPECS 518 TEMP =122.46 VFRAC=0 ; BLOCK D502 SEP2 ; Overhead - 511 MOLE-FRAC STREAM=511 SUBSTREAM=MIXED COMPS=ETHANOL FRACS=.826 FLASH-SPECS 511 TEMP=92.404 VFRAC=1 ; ; Bottoms 516 MOLE-FRAC STREAM=516 SUBSTREAM=MIXED COMPS=ETHANOL FRACS=.0002 FRAC STREAM=516 SUBSTREAM=MIXED COMPS= & GLUCOSE XYLOSE SOLSLDS ARABINOS GALACTOS MANNOSE GLUCOLIG & CELLOB XYLOLIG MANOLIG GALAOLIG ARABOLIG XYLITOL GLYCEROL & SUCCACID OIL CO2 H2SO4 N2 O2 SO2 & AACID FURFURAL HMF NH3 CSL CNUTR LACID & LGNSOL EXTRACT PROTEIN & FRACS= & 1 1 1 1 1 1 1 & 1 1 1 1 1 1 1 & 1 1 1 1 1 1 1 & 1 1 1 1 1 1 1 & 1 1 1 ; FRAC STREAM=516 SUBSTREAM=CISOLID COMPS= & CELLULOS XYLAN LIGNIN CELLULAS BIOMASS ZYMO GYPSUM ASH & TAR ARABINAN MANNAN & FRACS=1 1 1 1 1 1 1 1 & 1 1 1 FLASH-SPECS 516 TEMP=120.91 VFRAC=0 ; BLOCK H506- HEATER DESCRIPTION "Process side of EtOH Superheater before Mole Sieve" PARAM PRES=0 T=116 ; BLOCK H506+ HEATER DESCRIPTION "Steam side of EtOH Superheater before Mole Sieve" PARAM PRES=0.0 VFRAC=0.0 ; ; AS PER THE DELTA-T SIMULATION BLOCK T507-8 SEP2 DESCRIPTION "MOLE SIEVE" ; Overheads FRAC STREAM=515A SUBSTREAM=MIXED COMPS=ETHANOL FRACS=.15 ; Bottoms FRAC STREAM=514 SUBSTREAM=MIXED COMPS= & H2O GLUCOSE XYLOSE AACID H2SO4 FURFURAL HMF CO2 & CELLULOS O2 N2 NH3 CSL CNUTR LACID & FRACS=.005 1 1 1 1 1 1 1 & 1 1 1 1 1 1 1 FRAC STREAM=514 SUBSTREAM=CISOLID COMPS= & CELLULOS & FRACS=1 ; ; BLOCK H503 HEATER DESCRIPTION "COOL DOWN SEPARATED WATER & REGEN LOSSES" PARAM TEMP=35 PRES=2 ; BLOCK H507- HEATER DESCRIPTION "PROD/REGEN RECYCLE INTERCHANGER, PROD SIDE" PARAM PRES=22.5 ; BLOCK H507+ HEATER DESCRIPTION "PROD/REGEN RECYCLE INTERCHANGER, REGEN SIDE" PARAM PRES=1.44 T=91.7 ; BLOCK H509 HEATER DESCRIPTION "Product Ethanol Condenser and Cooler after Mole Sieve" PARAM TEMP=38 PRES=1 ; BLOCK H502 HEATER DESCRIPTION "D502 REBOILER - STEAM DEMAND" PARAM PRES=0.0 VFRAC=0.0 ; BLOCK H501 HEATER DESCRIPTION "D501 REBOILER - STEAM DEMAND" PARAM PRES=0.0 VFRAC=0.0 ; BLOCK RECTDUP DUPL DESCRIPTION "DUPLICATES QCD502 FOR EVAPORATOR AND CW CAPITAL" ; BLOCK E501LOSS FSPLIT DESCRIPTION "HEAT LOSS IN 1ST EFFECT" FRAC QE501L .02 ; BLOCK E502LOSS FSPLIT DESCRIPTION "HEAT LOSS IN 2ND EFFECT" FRAC QE502L .02 ; BLOCK E503LOSS FSPLIT DESCRIPTION "HEAT LOSS IN 3RD EFFECT" FRAC QE503L .02 ; BLOCK E501MIX MIXER DESCRIPTION "MIXES CONDENSATE FROM EVAPORATOR" PARAM PRES= 2 ; BLOCK E501WW FSPLIT DESCRIPTION "SPECIFIES FLOW TO WASTEWATER TREATMENT" FRAC 535 0.1 ; BLOCK E501SPT FSPLIT DESCRIPTION "SPLITS CONDENSATE RECYCLE" PARAM PRES = 3 DEF-KEY KEYNO=1 SUBSTREAM=MIXED COMPS=H2O MASS-FLOW 102 18000 1 MASS-FLOW 211 2000 1 ; MOLE-FLOW 243 3000 1 ; MASS-FLOW 245 41000 1 ; BLOCK E502V HEATER DESCRIPTION "2ND EFFECT CONDENSER" PARAM VFRAC=0 DELT=0 ; BLOCK E503V HEATER DESCRIPTION "3RD EFFECT CONDENSER" PARAM VFRAC=0 DELT=0 ; BLOCK H517 HEATER DESCRIPTION "FINAL CONDENSER ON EVAPORATOR" PARAM VFRAC=0 DELT=0 ; BLOCK E501LB HEATER DESCRIPTION "AUXILIARY STEAM CONDENSOR" PARAM PRES=.0 VFRAC=.0 ; BLOCK E501L FLASH2 DESCRIPTION "1ST EFFECT LIQUID SIDE" PROPERTIES NRTL-HOC PARAM PRES=0.384 ; BLOCK E502L FLASH2 DESCRIPTION "2ND EFFECT LIQUID SIDE" PROPERTIES NRTL-HOC PARAM PRES=0.289 ; BLOCK E503L FLASH2 DESCRIPTION "3rd EFFECT LIQUID SIDE" PROPERTIES NRTL-HOC PARAM PRES=0.211 ; BLOCK VNTMIX MIXER DESCRIPTION "VENT MIXER" ; BLOCK VNTSCRUB RADFRAC PARAM NSTAGE=4 FEEDS 524 1 / 523 4 ON-STAGE PRODUCTS 550 1 V / 551 4 L P-SPEC 1 0.9 COL-SPECS Q1=0 QN=0 MOLE-RDV=1 ; BLOCK MPOW5 MIXER DESCRIPTION "AREA 5000 MISCELLANEOUS WORK SUMMER" ; BLOCK DCOOL2 HEATER DESCRIPTION "DUMMY COOLER / AMBIENT COOLING IN S505" PARAM TEMP=40. PRES=.0 ; BLOCK T530 FSPLIT DESCRIPTION "RECYCLE WATER AND WWT LIQUID SEPARATOR" FRAC 580 .750 ; BLOCK S505 SEP2 DESCRIPTION "BEER BOTTOMS PNEUMAPRESS" ; Formerly centrifuges PARAM PRES=3.20 ;THE FRACTIONAL SPLITS ARE BASED ON THE PDU VENDOR TESTS ;THAT SHOWED AN OUTLET SOLIDS CONCENTRATION OF ;30% AND 98% RECOVERY OF INSOLUBLE SOLIDS FOR CENTRIFUGES. ;SOLUBLE COMPONENTS ARE SPLIT SO THAT THE LIQUID FRACTION OF ;EACH STREAM HAS THE SAME COMPOSITION. FRAC STREAM=571B SUBSTREAM=MIXED COMPS= & H2O ETHANOL FURFURAL HMF H2SO4 N2 CO2 O2 CH4 & NO NO2 NH3 SOLSLDS GLUCOSE XYLOSE GALACTOS & MANNOSE ARABINOS UNKNOWN AACID LACID CNUTR WNUTR & CSL OIL DENAT GLUCOLIG CELLOB XYLOLIG MANOLIG & GALAOLIG ARABOLIG ACETOLIG GLYCEROL SUCCACID & XYLITOL LGNSOL EXTRACT PROTEIN & FRACS=.10 .10 .10 .10 .10 .10 .10 .10 .10 & .10 .10 .10 .10 .10 .10 .10 & .10 .10 .10 .10 .10 1. 1. & 1. .10 .10 .10 .10 .10 .10 & .10 .10 .10 .10 .10 & .10 .10 .10 .10 ;KI 3/22/02: ;ALL WNUTR, CNUTR & CSL SHOULD HAVE BEEN CONSUMED & ;SO ANY REMAINING SHOULD GO OFF TO WWT SO THAT THE RECYCLE WILL BE ;CORRECT. ; FRAC STREAM=571B SUBSTREAM=CISOLID COMPS=CELLULOS XYLAN & ARABINAN MANNAN GALACTAN LIGNIN BIOMASS CELLULAS & ZYMO CASO4 CAH2O2 GYPSUM TAR ACETATE ASH & FRACS= .980 .980 & .980 .980 .980 .980 .50 .50 & 0.50 0.980 0.980 0.980 .98 .980 0.98 ; BLOCK M505 COMPR DESCRIPTION "AIR COMPRESSOR FOR POST-D PNEUMAPRESS SYSTEM" PARAM TYPE=ISENTROPIC DELP=125. SEFF=0.72 ; BLOCK M505COOL HEATER DESCRIPTION "COOLER FOR COMPRESSED PNEUMAMPRESS AIR" ; PARAM PRES=1.0 TEMP=40.0 PARAM TEMP=40.0 ; BLOCK S505FLSH FLASH2 DESCRIPTION "AIR-SOLIDS CONTACT IN PNEUMAPRESS" PARAM PRES=.0 DUTY=.0 ; BLOCK RWSPLT FSPLIT DESCRIPTION "RECYCLE WATER SPLITTER" FRAC 219 0.8/430 .001 ;THE FRACTIONS LISTED ARE ASSUMPTIONS. THE ACTUAL VALUES ARE ;DETERMINED BY THE FORTRAN BLOCK RECYCLE. ; BLOCK FWMIX MIXER DESCRIPTION "TANK T-530 FOR MIXING FRESH H2O AND RECYCLE H2O" PARAM NPHASE=1 PHASE=L ; ;------------------------------------------------------------ ; DIGESTION (WASTE WATER TREATMENT) BLOCKS - AREA 600 ;---------------------------------------------------------- ; BLOCK S600 MIXER DESCRIPTION "TANK T-603 TO MIX PROCESS WASTEWATER AND OTHER WASTES" PARAM PRES=2 ; BLOCK T610 SSPLIT DESCRIPTION "CLARIFIER" FRAC MIXED 625 0.1 FRAC CISOLID 625 1.0 ; BLOCK S614 SSPLIT DESCRIPTION "DEWATERING BELT FILTER PRESS" FRAC MIXED 623 0.1 FRAC CISOLID 623 1.0 ; BLOCK H602 HEATER DESCRIPTION "COOLER TO BRING WASTEWATER TO ANAEROBIC TEMP" PARAM TEMP=35.0 PRES=.0 ; BLOCK T608 RSTOIC DESCRIPTION "AEROBIC DIGESTOR" PARAM TEMP=21.1 PRES=1.0 STOIC 1 MIXED O2 -6.0 / GLUCOLIG -1.0 / H2O 5.0 / CO2 6.0 STOIC 2 MIXED O2 -12.0 / CELLOB -1.0 / H2O 11.0 / CO2 12.0 STOIC 3 MIXED O2 -6.0 / GLUCOSE -1.0 / H2O 6.0 / CO2 6.0 STOIC 4 MIXED O2 -6.0 / HMF -1.0 / H2O 3.0 / CO2 6.0 STOIC 5 MIXED O2 -5.0 / XYLOLIG -1.0 / H2O 4.0 / CO2 5.0 STOIC 6 MIXED O2 -5.0 / XYLOSE -1.0 / H2O 5.0 / CO2 5.0 STOIC 7 MIXED O2 -5.0 / FURFURAL -1.0 / H2O 2.0 / CO2 5.0 STOIC 8 MIXED O2 -6.0 / MANOLIG -1.0 / H2O 5.0 / CO2 6.0 STOIC 9 MIXED O2 -6.0 / MANNOSE -1.0 / H2O 6.0 / CO2 6.0 STOIC 10 MIXED O2 -6.0 / GALAOLIG -1.0 / H2O 5.0 / CO2 6.0 STOIC 11 MIXED O2 -6.0 / GALACTOS -1.0 / H2O 6.0 / CO2 6.0 STOIC 12 MIXED O2 -5.0 / ARABOLIG -1.0 / H2O 4.0 / CO2 5.0 STOIC 13 MIXED O2 -5.0 / ARABINOS -1.0 / H2O 5.0 / CO2 5.0 STOIC 15 MIXED O2 -2.0 / ACETOLIG -1.0 / H2O 2.0 / CO2 2.0 STOIC 16 MIXED O2 -2.0 / AACID -1.0 / H2O 2.0 / CO2 2.0 STOIC 17 MIXED O2 -3.0 / LACID -1.0 / H2O 3.0 / CO2 3.0 STOIC 18 MIXED O2 -.50 / UNKNOWN -1.0 / H2O .50 / CO2 .50 STOIC 19 MIXED SOLSLDS -1.0 / O2 1.19358 / H2O .011481 / CO2 1.0 / NO2 0.37314 / SO2 .00267 STOIC 20 MIXED O2 -3.0 / ETHANOL -1.0 / H2O 3.0 / CO2 2.0 STOIC 21 MIXED O2 -3.50 / GLYCEROL -1.0 / H2O 4.0 /CO2 3.0 STOIC 22 MIXED O2 -3.50 / SUCCACID -1.0 / H2O 3.0 /CO2 4.0 STOIC 23 MIXED O2 -5.50 / XYLITOL -1.0 / H2O 6.0 / CO2 5.0 STOIC 24 MIXED O2 -2.75 / MIXED NH4ACET -1.0 / MIXED H2O 3.5 / CO2 2.0 / N2 0.5 ; STOIC 25 MIXED GLUCOSE -1 / CISOLID BIOMASS 7.75281869 STOIC 26 MIXED MANNOSE -1 / CISOLID BIOMASS 7.75281869 STOIC 27 MIXED GALACTOS -1 / CISOLID BIOMASS 7.75281869 STOIC 28 MIXED XYLOSE -1.0 / CISOLID BIOMASS 6.46062489 STOIC 29 MIXED ARABINOS -1.0 / CISOLID BIOMASS 6.46062489 STOIC 30 MIXED XYLITOL -1.0 / CISOLID BIOMASS 6.54746538 STOIC 31 MIXED SOLSLDS -1.0 / CISOLID BIOMASS 4.2924 STOIC 32 MIXED UNKNOWN -1.0 / CISOLID BIOMASS 0.64607109 STOIC 33 MIXED GLUCOLIG -1.0 / CISOLID BIOMASS 6.977597 STOIC 34 MIXED GALAOLIG -1.0 / CISOLID BIOMASS 6.977597 STOIC 35 MIXED MANOLIG -1.0 / CISOLID BIOMASS 6.977597 STOIC 36 MIXED XYLOLIG -1.0 / CISOLID BIOMASS 5.685454 STOIC 37 MIXED CELLOB -1.0 / CISOLID BIOMASS 14.730461 STOIC 38 MIXED FURFURAL -1 / CISOLID BIOMASS 4.134923 STOIC 39 MIXED HMF -1.0 / CISOLID BIOMASS 5.4269558 STOIC 40 MIXED AACID -1.0 / CISOLID BIOMASS 2.584288 STOIC 41 MIXED LACID -1.0 / CISOLID BIOMASS 3.876431 STOIC 42 MIXED SUCCACID -1.0 / CISOLID BIOMASS 5.081824 STOIC 43 MIXED GLYCEROL -1.0 / CISOLID BIOMASS 3.963182 STOIC 44 MIXED OIL -1.0 / CISOLID BIOMASS 12.155542 STOIC 45 MIXED ETHANOL -1.0 / CISOLID BIOMASS 1.982524 STOIC 46 MIXED NH4ACET -1.0 / CISOLID BIOMASS 3.317135 STOIC 47 MIXED EXTRACT -1.0 / O2 1.19358 / H2O .011481 / CO2 1.0 / NO2 0.37314 / SO2 .00267 STOIC 48 MIXED PROTEIN -1.0 / O2 1.19358 / H2O .011481 / CO2 1.0 / NO2 0.37314 / SO2 .00267 STOIC 49 MIXED EXTRACT -1.0 / CISOLID BIOMASS 4.2924 STOIC 50 MIXED PROTEIN -1.0 / CISOLID BIOMASS 4.2924 ; CONV 1 MIXED GLUCOLIG 0.6 CONV 2 MIXED CELLOB 0.6 CONV 3 MIXED GLUCOSE 0.6 CONV 4 MIXED HMF 0.6 CONV 5 MIXED XYLOLIG 0.6 CONV 6 MIXED XYLOSE 0.6 CONV 7 MIXED FURFURAL 0.6 CONV 8 MIXED MANOLIG 0.6 CONV 9 MIXED MANNOSE 0.6 CONV 10 MIXED GALAOLIG 0.6 CONV 11 MIXED GALACTOS 0.6 CONV 12 MIXED ARABOLIG 0.6 CONV 13 MIXED ARABINOS 0.6 CONV 15 MIXED ACETOLIG 0.6 CONV 16 MIXED AACID 0.6 CONV 17 MIXED LACID 0.6 CONV 18 MIXED UNKNOWN 0.6 CONV 19 MIXED SOLSLDS 0.6 CONV 20 MIXED ETHANOL 0.6 CONV 21 MIXED GLYCEROL 0.6 CONV 22 MIXED SUCCACID 0.6 CONV 23 MIXED XYLITOL 0.6 CONV 24 MIXED NH4ACET 0.6 ; CONV 25 MIXED GLUCOSE 0.3 CONV 26 MIXED MANNOSE 0.3 CONV 27 MIXED GALACTOS 0.3 CONV 28 MIXED XYLOSE 0.3 CONV 29 MIXED ARABINOS 0.3 CONV 30 MIXED XYLITOL 0.3 CONV 31 MIXED SOLSLDS 0.3 CONV 32 MIXED UNKNOWN 0.3 CONV 33 MIXED GLUCOLIG 0.3 CONV 34 MIXED GALAOLIG 0.3 CONV 35 MIXED MANOLIG 0.3 CONV 36 MIXED XYLOLIG 0.3 CONV 37 MIXED CELLOB 0.3 CONV 38 MIXED FURFURAL 0.3 CONV 39 MIXED HMF 0.3 CONV 40 MIXED AACID 0.3 CONV 41 MIXED LACID 0.3 CONV 42 MIXED SUCCACID 0.3 CONV 43 MIXED GLYCEROL 0.3 CONV 44 MIXED OIL 0.3 CONV 45 MIXED ETHANOL 0.3 CONV 46 MIXED NH4ACET 0.3 ; CONV 47 MIXED EXTRACT 0.6 CONV 48 MIXED PROTEIN 0.6 CONV 49 MIXED EXTRACT 0.3 CONV 50 MIXED PROTEIN 0.3 ; BLOCK T606FLSH FLASH2 DESCRIPTION "FLASH FOR ANAEROBIC DIGESTION" PARAM PRES=1.0 DUTY=.0 ; BLOCK NUTMIX MIXER DESCRIPTION "ADDS CHEMICALS AND NUTRIENTS TO ANAEROBIC DIGESTION" ; BLOCK T608FLSH FLASH2 DESCRIPTION "FLASH FOR AEROBIC TREATMENT" PARAM PRES=.0 DUTY=.0 ; BLOCK MPOW6 MIXER DESCRIPTION "AREA 6000 MISCELLANEOUS WORK SUMMER" ; BLOCK T606 USER DESCRIPTION "Anaerobic Digester" SUBROUTINE USRAN4 PARAM NREAL=5 REAL VALUE-LIST=0.9 1.0 0.03 0.75 1.0 FLASH-SPECS 613C TP TEMP=95 PRES=1 ; ;----------------------------------------------------------- ; STORAGE BLOCKS - AREA 700 ;----------------------------------------------------------- ; BLOCK DCOOLE HEATER DESCRIPTION "DUMMY COOLER TO SET ETHANOL DENSITY" PARAM TEMP=20.0 PRES=.0 ; BLOCK PRODMIX MIXER DESCRIPTION "ETHANOL AND DENATURANT MIXER" PARAM PRES=1.0 ; BLOCK TSTORE MIXER DESCRIPTION "GENERAL STORAGE TANK" ; ;-------------------------------------------------------------- ; BOILER BLOCKS - AREA 800 ;------------------------------------------------------------- ; BLOCK M802MIX MIXER DESCRIPTION "MIX PNEUMAPRESS VENTS AND INCOMING AIR" ; BLOCK M802 COMPR DESCRIPTION "COMBUSTION FAN" PARAM TYPE=ISENTROPIC PRES=1.0138849 SEFF=.750 NPHASE=2 & SB-MAXIT=100 ; BLOCK M801MIX MIXER DESCRIPTION "SLURRY MIXER" PARAM PRES=1.0 ; BLOCK M804 SSPLIT DESCRIPTION "BAGHOUSE FOR THE BOILER" ;EFFICIENCY LOSS IS BASED ON HAMON-COTTRELL (VENDOR) QUOTE IN ;REI 1998 SUBCONTRACT FRAC MIXED 810 1.0 FRAC CISOLID 809 0.988 ; BLOCK QCOMSPLT FSPLIT ;EFFICIENCY LOSS IS FROM FOSTER WHEELER (VENDOR) QUOTE IN ;REI 1998 SUBCONTRACT DESCRIPTION & "ACCOUNT FOR 1% RADIANT LOSSES AND 1.5% UNACCOUNTED" FRAC QCOMLOSS .026 ; BLOCK M803HEAT HEATER DESCRIPTION "GAS SIDE OF STEAM BOILER" PARAM TEMP=278.3 PRES=.0 ; BLOCK H801+ HEATER PARAM TEMP=157 PRES=0.0 ; BLOCK H801- HEATER PARAM PRES=0.0 ; BLOCK M801STM HEATER PARAM TEMP=120 VFRAC=0.0 ; BLOCK M801FLSH FLASH2 DESCRIPTION "CAKE DRYER PRIOR TO BOILER" PROPERTIES NRTL-HOC PARAM PRES=1.0 ; BLOCK M801CND HEATER DESCRIPTION "DRYER OFFGAS CONDENSER" PARAM TEMP=50 PRES=1.0 ; BLOCK M803CMB RSTOIC DESCRIPTION "FLUID BED BOILER COMBUSTOR" PARAM TEMP=870.0 PRES=-.03402298 NPHASE=1 SERIES=YES STOIC 1 MIXED CH4 -1.0 / O2 -2.0 / CO2 1.0 / H2O 2.0 STOIC 2 CISOLID CELLULOS -1.0 / MIXED O2 -6.0 / H2O & 5.0 / CO2 6.0 STOIC 3 CISOLID XYLAN -1.0 / MIXED O2 -5.0 / CO2 5.0 & / H2O 4.0 STOIC 4 CISOLID ARABINAN -1.0 / MIXED O2 -5.0 / CO2 & 5.0 / H2O 4.0 STOIC 5 CISOLID MANNAN -1.0 / MIXED O2 -6.0 / H2O 5.0 & / CO2 6.0 STOIC 6 CISOLID LIGNIN -1.0 / MIXED O2 -12.825 / H2O & 6.950 / CO2 10.0 STOIC 8 CISOLID ACETATE -1.0 / MIXED O2 -2.0 / CO2 2.0 & / H2O 2.0 STOIC 7 CISOLID GALACTAN -1.0 / MIXED O2 -6.0 / H2O & 5.0 / CO2 6.0 STOIC 9 MIXED O2 -6.0 / GLUCOLIG -1.0 / H2O 5.0 / CO2 & 6.0 STOIC 10 MIXED CELLOB -1.0 / O2 -12.0 / CO2 12.0 / & H2O 11.0 STOIC 11 MIXED GLUCOSE -1.0 / O2 -6.0 / CO2 6.0 / H2O & 6.0 STOIC 12 MIXED HMF -1.0 / O2 -6.0 / H2O 3.0 / CO2 & 6.0 STOIC 13 MIXED XYLOLIG -1.0 / O2 -5.0 / H2O 4.0 / CO2 & 5.0 STOIC 14 MIXED XYLOSE -1.0 / O2 -5.0 / H2O 5.0 / CO2 & 5.0 STOIC 15 MIXED FURFURAL -1.0 / O2 -5.0 / H2O 2.0 / & CO2 5.0 STOIC 16 CISOLID TAR -1.0 / MIXED O2 -5.0 / H2O 5.0 / & CO2 5.0 STOIC 17 MIXED MANOLIG -1.0 / O2 -6.0 / H2O 5.0 / CO2 & 6.0 STOIC 18 MIXED MANNOSE -1.0 / O2 -6.0 / H2O 6.0 / CO2 & 6.0 STOIC 19 MIXED GALAOLIG -1.0 / O2 -6.0 / H2O 5.0 / & CO2 6.0 STOIC 20 MIXED GALACTOS -1.0 / O2 -6.0 / H2O 6.0 / & CO2 6.0 STOIC 21 MIXED ARABOLIG -1.0 / O2 -5.0 / H2O 4.0 / & CO2 5.0 STOIC 22 MIXED ARABINOS -1.0 / O2 -5.0 / H2O 5.0 / & CO2 5.0 STOIC 23 MIXED ACETOLIG -1.0 / O2 -2.0 / H2O 2.0 / & CO2 2.0 STOIC 24 MIXED AACID -1.0 / O2 -2.0 / H2O 2.0 / CO2 & 2.0 STOIC 25 MIXED LACID -1.0 / O2 -3.0 / H2O 3.0 / CO2 & 3.0 STOIC 26 CISOLID CELLULAS -1.0 / MIXED O2 -1.24450 / & H2O .7850 / CO2 1.0 / N2 .1450 / SO2 .0070 STOIC 27 MIXED SOLSLDS -1.0 / O2 1.56672 / H2O .011481 / & CO2 1.0 / N2 0.18657 / SO2 .00267 STOIC 28 MIXED ETHANOL -1.0 / O2 -3.0 / H2O 3.0 / CO2 & 2.0 STOIC 29 CISOLID ZYMO -1.0 / MIXED O2 -1.20 / H2O .90 & / CO2 1.0 / N2 .10 STOIC 30 MIXED GLYCEROL -1.0 / O2 -3.50 / H2O 4.0 / & CO2 3.0 STOIC 31 MIXED SUCCACID -1.0 / O2 -3.50 / H2O 3.0 / & CO2 4.0 STOIC 32 MIXED XYLITOL -1.0 / O2 -5.50 / H2O 6.0 / & CO2 5.0 STOIC 33 CISOLID BIOMASS -1.0 / MIXED O2 -1.21850 / H2O & .820 / CO2 1.0 / N2 .1150 / SO2 .00350 STOIC 105 MIXED SO2 -1.0 / O2 -.50 / H2O -1.0 / H2SO4 & 1.0 STOIC 66 MIXED H2S -1.0 / O2 -1.50 / SO2 1.0 / H2O & 1.0 STOIC 67 MIXED N2 -.50 / O2 -1.0 / NO2 1.0 STOIC 99 MIXED H2SO4 -1.0 / SO2 1.0 / H2O 1.0 / O2 & .50 STOIC 100 MIXED NH4SO4 -1.0 / MIXED O2 -1.0 / SO2 & 1.0 / N2 1.0 / H2O 4.0 STOIC 34 MIXED OIL -1 / O2 -25.5 / CO2 18 / H2O 17 STOIC 35 MIXED NH4ACET -1/MIXED O2 -2.75/CO2 2/H2O 3.5/N2 0.5 STOIC 36 MIXED EXTRACT -1.0 / O2 1.56672 / H2O .011481 / & CO2 1.0 / N2 0.18657 / SO2 .00267 STOIC 37 MIXED PROTEIN -1.0 / O2 1.56672 / H2O .011481 / & CO2 1.0 / N2 0.18657 / SO2 .00267 STOIC 40 MIXED CO2 -1 / CO 1 / O2 0.5 STOIC 45 MIXED LGNSOL -1.0 / MIXED O2 -12.825 / H2O & 6.950 / CO2 10.0 CONV 1 MIXED CH4 0.99 CONV 2 CISOLID CELLULOS .99 CONV 3 CISOLID XYLAN .99 CONV 4 CISOLID ARABINAN .99 CONV 5 CISOLID MANNAN .99 CONV 6 CISOLID LIGNIN .99 CONV 8 CISOLID ACETATE .99 CONV 7 CISOLID GALACTAN .99 CONV 9 MIXED GLUCOLIG .99 CONV 10 MIXED CELLOB .99 CONV 11 MIXED GLUCOSE .99 CONV 12 MIXED HMF .99 CONV 13 MIXED XYLOLIG .99 CONV 14 MIXED XYLOSE .99 CONV 15 MIXED FURFURAL .99 CONV 16 CISOLID TAR .99 CONV 17 MIXED MANOLIG .99 CONV 18 MIXED MANNOSE .99 CONV 19 MIXED GALAOLIG .99 CONV 20 MIXED GALACTOS .99 CONV 21 MIXED ARABOLIG .99 CONV 22 MIXED ARABINOS .99 CONV 23 MIXED ACETOLIG .99 CONV 24 MIXED AACID .99 CONV 25 MIXED LACID .99 CONV 26 CISOLID CELLULAS .99 CONV 28 MIXED ETHANOL .99 CONV 29 CISOLID ZYMO .99 CONV 30 MIXED GLYCEROL .99 CONV 31 MIXED SUCCACID .99 CONV 32 MIXED XYLITOL .99 CONV 33 CISOLID BIOMASS .99 CONV 35 MIXED NH4ACET .99 CONV 27 MIXED SOLSLDS 0.99 CONV 36 MIXED EXTRACT 0.99 CONV 37 MIXED PROTEIN 0.99 CONV 45 MIXED LGNSOL .99 CONV 105 MIXED SO2 .010 CONV 66 MIXED H2S 1.0 EXTENT 67 .0010 CONV 99 MIXED H2SO4 1.0 CONV 100 MIXED NH4SO4 1.0 CONV 34 MIXED OIL .99 EXTENT 40 0.0001 ; ;------------------------------------------------------------- ; TURBOGENERATOR BLOCKS - AREA 810 ;------------------------------------------------------------- ; BLOCK M811GEN FSPLIT DESCRIPTION & "THIS BLOCK IS THE ELECTRICAL PART OF THE TURBOGENERATOR" ;THE GENERATOR EFFICIENCY WAS ESTIMATED AT 96% ;EFFICIENCY LOSS IS FROM ABB (VENDOR) 1998 QUOTE IN ;REI 1999 SUBCONTRACT REPORT FRAC WTOTAL .96 ; BLOCK M811XSPT FSPLIT DESCRIPTION "XHP (86 ATM) STEAM SPLITTER" MASS-FLOW 812D 0.1 ; BLOCK M811HSPT FSPLIT DESCRIPTION "HP (150 PSIG) STEAM SPLITTER" FRAC 812B .050 MASS-FLOW 814 18758.0 ; BLOCK M811ISPT FSPLIT DESCRIPTION "IP (50 PSIG) STEAM SPLITTER" MASS-FLOW 815A 42000 ; FRAC 815A .050 MASS-FLOW 815 70000 ; BLOCK M811LSPT FSPLIT DESCRIPTION "LP (10 PSIG) STEAM SPLITTER" MASS-FLOW 860 1000 ; BLOCK H811+ HEATER DESCRIPTION "BOILER ECONOMIZER" PARAM TEMP=350 PRES=-0.68 ; BLOCK H811-A HEATER DESCRIPTION "BFW HEATER-SENSIBLE" PARAM PRES=-0.68 VFRAC=1.0 ; BLOCK H811-B HEATER DESCRIPTION "BFW HEATER-LATENT" PARAM PRES=0.0 VFRAC=0.0 ; BLOCK M803BD FLASH2 DESCRIPTION "STEAM SIDE OF THE FLUIDIZED BED BOILER" PARAM PRES=1414.7 VFRAC=.970 ; BLOCK M803SHTR HEATER DESCRIPTION "BOILER SUPERHEATER" PARAM TEMP=950 PRES=1264.7 ; BLOCK T826 FLASH2 DESCRIPTION "BOILER WATER DEAERATOR" PARAM PRES=-0.10 VFRAC=.0 ; BLOCK P826AS PUMP DESCRIPTION "BOILER FEED WATER PUMP" PARAM PRES=1444.7 ; BLOCK P824AS PUMP DESCRIPTION "CONDENSATE MAKE-UP PUMP" PARAM PRES=3.402 ; BLOCK P811AS PUMP DESCRIPTION "CONDENSATE PUMP" PARAM PRES=4.2 ; BLOCK M811HTRB COMPR DESCRIPTION "HIGH PRESSURE PART OF THE STEAM TURBINE" ;EFFICIENCIES ARE FROM ABB (VENDOR) QUOTE IN ;REI 1998 SUBCONTRACT PARAM TYPE=ISENTROPIC PRES=13 SEFF=.85 MEFF=0.98 & NPHASE=2 ; BLOCK M811ITRB COMPR DESCRIPTION "MEDIUM PRESSURE PART OF THE STEAM TURBINE" PARAM TYPE=ISENTROPIC PRES=4.4229877 SEFF=.85 MEFF=0.98 & NPHASE=2 SB-MAXIT=100 ; BLOCK M811LTRB COMPR DESCRIPTION "VACUUM PART OF THE STEAM TURBINE" PARAM TYPE=ISENTROPIC PRES=24.7 SEFF=.85 MEFF=0.98 & NPHASE=2 ; BLOCK M811VLRB COMPR DESCRIPTION "VACUUM PART OF THE STEAM TURBINE" PARAM TYPE=ISENTROPIC PRES=1.47 SEFF=.85 MEFF=0.98 & NPHASE=2 ; BLOCK M811CND HEATER DESCRIPTION "STEAM SYSTEM CONDENSOR" PARAM PRES=.0 VFRAC=.0 ; BLOCK T824AS MIXER DESCRIPTION "CONDENSATE SURGE DRUM MS-804" ; BLOCK MPOW8 MIXER DESCRIPTION "AREA 8000 MISCELLANEOUS WORK SUMMER" ; ;------------------------------------------------------------ ; UTILITY BLOCKS - AREA 900 ;------------------------------------------------------------ ; BLOCK CHCWDUP DUPL DESCRIPTION "DUPLICATES QH914 FOR CHW AND CW CAPITAL & OP COSTING" ; BLOCK QTDUP DUPL DESCRIPTION "DUPLICATES QTTOTAL FOR CW CAPITAL & OP COSTING" ; BLOCK CWDUP DUPL DESCRIPTION "DUPLICATES QH14BCW FOR CW CAPACITY AND EVAPORATION" ; BLOCK AGITAT MIXER DESCRIPTION "MIXES THE AGITATOR POWER REQUIREMENTS" ; BLOCK CHCWMIX MIXER DESCRIPTION "SSCF & SEED CHW/CW DEMAND MIXER" ; BLOCK COMPWK MIXER DESCRIPTION "COMPRESSOR WORK DEMAND CALCULATOR" ; BLOCK HEATCHW- MIXER DESCRIPTION "CHILLED WATER HEAT DEMAND MIXER" ; BLOCK SSCFCW MIXER DESCRIPTION "SSCF COOLING WATER DEMAND MIXER" ; BLOCK HEATCW-S MIXER DESCRIPTION "COOLING WATER HEAT DEMAND MIXER" ; BLOCK PMPWK MIXER DESCRIPTION "PUMP WORK DEMAND CALCULATOR" ; BLOCK WKMIX MIXER DESCRIPTION "OVERALL NET WORK CALCULATOR FOR THE PLANT" ; BLOCK WKSEP MIXER DESCRIPTION "OVERALL NET WORK USED BY THE PLANT" ; BLOCK QCWMIX MIXER DESCRIPTION "CW CAPITAL HEAT DEMAND MIXER" ; BLOCK QCHWMIX MIXER DESCRIPTION "CHILLED WATER CAPITAL HEAT DEMAND MIXER" ; BLOCK ASPLT FSPLIT DESCRIPTION "FERMENTATION AIR SPLITTER" FRAC 413 .90 ; Controlled by fortran AIRREQ ; BLOCK CIPCS MIXER DESCRIPTION "CIP/CS SYSTEM TANKS AND PUMPS" ; BLOCK T914 MIXER DESCRIPTION "DUMMY BLOCK TO CALCULATE TOTAL WATER DEMAND" ; BLOCK CHILWAT HEATER DESCRIPTION "CHILLED WATER REQUIREMENT CALC" PARAM PRES=.0 DELT=4.0 ; BLOCK CWATCAP HEATER DESCRIPTION "COOLING WATER REQUIREMENT CALC FOR CAPITAL COST" PARAM PRES=.0 DELT=9. ; BLOCK CWATOP HEATER DESCRIPTION "COOLING WATER REQUIREMENT CALC FOR OPERATING COST" PARAM PRES=.0 DELT=9. ; BLOCK H910 HEATER DESCRIPTION "WATER STERILIZER" PARAM TEMP=121. PRES=0.0 ; BLOCK H914 HEATER DESCRIPTION "WELL WATER COOLER FOR SSCF BROTH" PARAM TEMP=26. PRES=0.0 ; BLOCK CWFLSH HEATER DESCRIPTION "COOLING TOWER FLASH CALC" PARAM TEMP=28.0 VFRAC=1.0 ; BLOCK CLTWR MIXER DESCRIPTION "DUMMY BLOCK FOR COOLING TOWWER FLOWS" ; BLOCK ACOMP COMPR DESCRIPTION "AIR COMPRESSOR FOR FERMENTATIONS" PARAM TYPE=ISENTROPIC PRES=3. ; BLOCK AFLSH HEATER DESCRIPTION "PRESSURE REDUCER FOR FERMENTATION AIR" PARAM PRES=1.0 TEMP=40.0 ; BLOCK CHEMIX MIXER DESCRIPTION "BLOCK TO CALC CHEM'S FOR BOILER & COOLING TOWER" ; BLOCK QH14BSP FSPLIT DESCRIPTION "SETS FRACTION OF YEAR THAT CHW IS REQ. FOR SSCF COOLING" FRAC QH14BCHW 0.00000001 ; BLOCK MPOW10 MIXER DESCRIPTION "AREA 10000 MISCELLANEOUS WORK SUMMER" ; BLOCK AIRCMP MIXER DESCRIPTION "TOTAL COMPRESSED AIR REQUIRED" ; Does not include cellulase air requirement ; BLOCK MPOWTOT MIXER DESCRIPTION "TOTAL MISCELLANEOUS POWER SUMMER" ; BLOCK SSCFSDCW MIXER DESCRIPTION "SSCF SEED TRAIN HEAT MIXER" ; ;----------------------------------------------------------------------- ; DESIGN SPECIFICATIONS ; PRETREATMENT DESIGN-SPECS ;------------------------------------------------------------------------ ; DESIGN-SPEC ACIDCONC ;CONTROLS THE ACID CONCENTRATION OF STREAM 217 DEFINE ACIDFL MASS-FLOW STREAM=217 SUBSTREAM=MIXED & COMPONENT=H2SO4 DEFINE WATFLW MASS-FLOW STREAM=217 SUBSTREAM=MIXED & COMPONENT=H2O F ACDCNC = ACIDFL/(WATFLW+ACIDFL) ; SPEC "ACDCNC" TO "SETACD" SPEC "ACDCNC" TO "0.011" TOL-SPEC "0.00001" VARY STREAM-VAR STREAM=212 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "100" "10000" ; DESIGN-SPEC LPSTMFLO ;CONTROLS THE AMOUNT OF LP STEAM TO PRETREATMENT TO ;ACHIEVE 100 C. DEFINE THTR INFO-VAR INFO=HEAT VAR=DUTY STREAM=QM202LO SPEC "THTR" TO "0" TOL-SPEC "10.0" VARY STREAM-VAR STREAM=215 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "100" "500000" ; DESIGN-SPEC REACHEAT ;CALCULATES THE AMOUNT OF HP STEAM REQUIRED TO OBTAIN ;THE CORRECT RXN TEMPERATURE IN PRETREATMENT. DEFINE QRXNXS INFO-VAR INFO=HEAT VAR=DUTY STREAM=QM202HI SPEC "QRXNXS" TO "0" TOL-SPEC "5" VARY STREAM-VAR STREAM=216 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "200" "100000" ; DESIGN-SPEC CT-S205A DEFINE SOL225 STREAM-VAR STREAM=225 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WAT225 STREAM-VAR STREAM=225 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; The spec of 0.548 is from Pneumapress Test #9 ; under the Harris 2000 subcontract SPEC"SOL225/(SOL225+WAT225)" TO "0.548" TOL-SPEC"0.001" VARY BLOCK-VAR BLOCK=S205A SENTENCE=FRAC VARIABLE=FRAC & ID1=MIXED ID2=225 LIMITS "0.01" "1.0" ; DESIGN-SPEC CT-S205B DEFINE SOLID STREAM-VAR STREAM=255 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE OTHER STREAM-VAR STREAM=255 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; The spec of 0.548 is from Pneumapress Test #9 ; under the Harris 2000 subcontract SPEC "SOLID/(OTHER+SOLID)" TO "0.548" TOL-SPEC "0.001" VARY BLOCK-VAR BLOCK=S205B SENTENCE=FRAC VARIABLE=FRAC ID1=MIXED & MIXED ID2=256 ELEMENT=1 LIMITS "0.70" "0.999" ; DESIGN-SPEC CT-S222 DEFINE SOL229 STREAM-VAR STREAM=229 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WAT229 STREAM-VAR STREAM=229 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW SPEC"SOL229/(SOL229+WAT229)" TO "0.8" TOL-SPEC "0.001" VARY BLOCK-VAR BLOCK=S222 SENTENCE=FRAC VARIABLE=FRAC & ID1=MIXED ID2=229 LIMITS "0.0" "1.0" ; ;--------------------------------------------------------------- ; SACCHARIFICATION AND FERMENTATION DESIGN-SPECS ;--------------------------------------------------------------- ; DESIGN-SPEC SACCHHEAT ;THIS SPEC DETERMINES THE AMOUNT OF 50 PSIG STEAM ;REQ'D TO HEAT THE HYDROLZYATE SLURRY TO 65C FOR SACCHARIFICATION ; DEFINE QSACCH INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH301EX SPEC QSACCH TO 0 TOL-SPEC 10 VARY STREAM-VAR STREAM=590 SUBSTREAM=MIXED VARIABLE=MASS-FLOW LIMITS 10 20000 ; ;--------------------------------------------------------------- ; DISTILLAION DESIGN-SPECS ;--------------------------------------------------------------- ; DESIGN-SPEC SCRBFLOW DEFINE FRCETO MASS-FLOW STREAM=550 SUBSTREAM=MIXED COMPONENT=ETHANOL ; 40 ton/yr ethanol loss = 4.316kg/hr (8406 hr/yr) ; changed from 8400 hr/yr to 8406 by AA, 2/20/01 SPEC FRCETO TO 4.316 TOL-SPEC 0.0001 VARY STREAM-VAR STREAM=524 SUBSTREAM=MIXED VARIABLE=MASS-FLOW LIMITS 5000 40000 ; DESIGN-SPEC TRIM ;THIS SPEC DETERMINES THE AMOUNT OF 50 PSIG STEAM ;REQUIRED TO TRIM THE RECTIFICATION COLUMN. ; DEFINE QTRMO INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH504EX SPEC QTRMO TO 0 TOL-SPEC 10 VARY STREAM-VAR STREAM=592 SUBSTREAM=MIXED VARIABLE=MASS-FLOW LIMITS 1 100000 ; DESIGN-SPEC REBOIL ;THIS SPEC DETERMINES THE AMOUNT OF 150 PSIG STEAM ;REQ'D FOR THE BEER COLUMN REBOILER. ; DEFINE QREBO INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QRD501EX SPEC QREBO TO 0 TOL-SPEC 10 VARY STREAM-VAR STREAM=594 SUBSTREAM=MIXED VARIABLE=MASS-FLOW LIMITS 10000 200000 ; DESIGN-SPEC SUPRHET ;THIS SPEC DETERMINES THE AMOUNT OF 50 PSIG STEAM ;REQ'D TO SUPERHEAT THE ETHANOL INTO THE MOLECULAR SIEVE ; DEFINE QSUPE INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH506EX SPEC QSUPE TO 0 TOL-SPEC 10 VARY STREAM-VAR STREAM=596 SUBSTREAM=MIXED VARIABLE=MASS-FLOW LIMITS 10 20000 ; DESIGN-SPEC EV1SIZ ;CALCULATES THE PRESSURE FOR E501L TO MAKE THE HEAT-TRANSFER ;TO ALL EFFECTS THE SAME DEFINE Q0 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QC502A DEFINE Q0B INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE501A DEFINE Q1 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE502A DEFINE Q2 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE503A DEFINE T0 STREAM-VAR STREAM=511 SUBSTREAM=MIXED & VARIABLE=TEMP DEFINE T1 STREAM-VAR STREAM=526 SUBSTREAM=MIXED & VARIABLE=TEMP DEFINE T2 STREAM-VAR STREAM=529 SUBSTREAM=MIXED & VARIABLE=TEMP DEFINE T3 STREAM-VAR STREAM=532 SUBSTREAM=MIXED & VARIABLE=TEMP ; The heat transfer coefficient for the 1st stage is 135 Btu / ft^2 F ; The heat transfer coefficient for the 2nd and 3rd stages is 170 ; There are 2 1st & 3rd stages and 1 2nd stage ; Changes to the stages and heat transfer coefficients need to be made to ; EV2SIZ as well. MR 21 May 98 F QF1=(Q0+Q0B)/((T0-T1)*135) F QF2=Q1/((T1-T2)*0.5*170) F QF3=Q2/((T2-T3)*170) F QSET=(QF1+QF2+QF3)/3 F WRITE(NHSTRY,'("EV1SIZ")') F WRITE(NHSTRY,'('' QF1 = '',g12.5)')QF1 F WRITE(NHSTRY,'('' QF2 = '',g12.5)')QF2 F WRITE(NHSTRY,'('' QF3 = '',g12.5)')QF3 F WRITE(NHSTRY,'('' QSET = '',g12.5)')QSET SPEC "QF2" TO "QSET" TOLSPEC "1" VARY BLOCK-VAR BLOCK=E501L VARIABLE=PRES SENTENCE=PARAM LIMITS "0.5" "0.65" ; DESIGN-SPEC EV2SIZ ;CALCULATES THE PRESSURE FOR E502L TO MAKE THE HEAT-TRANSFER ;TO ALL EFFECTS THE SAME DEFINE Q0 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QC502A DEFINE Q0B INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE501A DEFINE Q1 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE502A DEFINE Q2 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE503A DEFINE T0 STREAM-VAR STREAM=511 SUBSTREAM=MIXED & VARIABLE=TEMP DEFINE T1 STREAM-VAR STREAM=526 SUBSTREAM=MIXED & VARIABLE=TEMP DEFINE T2 STREAM-VAR STREAM=529 SUBSTREAM=MIXED & VARIABLE=TEMP DEFINE T3 STREAM-VAR STREAM=532 SUBSTREAM=MIXED & VARIABLE=TEMP F QF1=(Q0+Q0B)/((T0-T1)*135) F QF2=Q1/((T1-T2)*0.5*170) F QF3=Q2/((T2-T3)*170) F QSET=(QF1+QF2+QF3)/3 F WRITE(NHSTRY,'("EV2SIZ")') F WRITE(NHSTRY,'('' QF1 = '',g12.5)')QF1 F WRITE(NHSTRY,'('' QF2 = '',g12.5)')QF2 F WRITE(NHSTRY,'('' QF3 = '',g12.5)')QF3 F WRITE(NHSTRY,'('' QSET = '',g12.5)')QSET SPEC "QF3" TO "QSET" TOLSPEC "1" VARY BLOCK-VAR BLOCK=E502L VARIABLE=PRES SENTENCE=PARAM LIMITS "0.25" "0.35" ; DESIGN-SPEC EVAPCONC ; SETS FLOW OF QE501A to set moisture concentration in 531 IN-UNITS MET ENTHALPY-FLO='MMKCAL/HR' DEFINE SOL531 STREAM-VAR STREAM=531 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE FLW531 STREAM-VAR STREAM=531 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE WAT531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED & COMPONENT=H2O SPEC "WAT531/(SOL531+FLW531)" TO "0.6" TOLSPEC "0.001" VARY INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE501A LIMITS "0.0" "50.0" ; DESIGN-SPEC MS-BTM ; Specification of 0.005 mass fraction H2O in product ethanol DEFINE WT514 MASS-FRAC STREAM=514 SUBSTREAM=MIXED COMPONENT=H2O SPEC WT514 TO 0.005 TOL-SPEC 0.0001 VARY BLOCK-VAR BLOCK=T507-8 SENTENCE=FRAC VARIABLE=FRACS & ID1=MIXED ID2=514 ELEMENT=1 LIMITS 0.001 0.3 ; DESIGN-SPEC MS-OVHD ; Specification of 0.7 mass frac ethanol in recycle to Rectification DEFINE ET515A MASS-FRAC STREAM=515A SUBSTREAM=MIXED COMPONENT=ETHANOL SPEC ET515A TO 0.722 TOL-SPEC 0.001 VARY BLOCK-VAR BLOCK=T507-8 SENTENCE=FRAC VARIABLE=FRACS & ID1=MIXED ID2=515A ELEMENT=1 LIMITS 0.05 0.5 ; DESIGN-SPEC D502BTMS ; Adjust mole-frac specification in D502 SEP2 to meet a specified ; MASS-FRAC DEFINE BTMETH MASS-FRAC STREAM=516 SUBSTREAM=MIXED COMPONENT=ETHANOL SPEC BTMETH TO .0005 TOL-SPEC .00001 VARY BLOCK-VAR BLOCK=D502 SENTENCE=MOLE-FRAC VARIABLE=FRACS & ID1=MIXED ID2=516 ELEMENT=1 LIMITS .0001 .1 DESIGN-SPEC D502OVHD ; Adjust mole-frac specification in D502 SEP2 to meet a specified ; MASS-FRAC DEFINE OVETOH MASS-FLOW STREAM=511 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE OVH2O MASS-FLOW STREAM=511 SUBSTREAM=MIXED COMPONENT=H2O SPEC "OVETOH/(OVETOH+OVH2O)" TO .9250 TOL-SPEC .0001 VARY BLOCK-VAR BLOCK=D502 SENTENCE=MOLE-FRAC VARIABLE=FRACS & ID1=MIXED ID2=511 ELEMENT=1 LIMITS .75 .999 ; DESIGN-SPEC CFUGE3S ; Varies the split of water and most of the mixed components ; to reach a specified solids fraction in 571. Works with ; fortran block CFUGESLD to vary not only water but several ; components ; DEFINE SOLIDS STREAM-VAR STREAM=571 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE TMIXED STREAM-VAR STREAM=571 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FH2O MASS-FLOW STREAM=571 SUBSTREAM=MIXED & COMPONENT=H2O ; DEFINE FCSL MASS-FLOW STREAM=571 SUBSTREAM=MIXED & ; COMPONENT=CSL ; DEFINE FGLUC MASS-FLOW STREAM=571 SUBSTREAM=MIXED & ; COMPONENT=GLUCOSE ; DEFINE FCNUTR MASS-FLOW STREAM=571 SUBSTREAM=MIXED & ; COMPONENT=CNUTR F RATIO = FH2O / (SOLIDS + TMIXED) F WRITE(NHSTRY,101)RATIO F 101 FORMAT(' Cfuge 3 Design Spec',/,' Fraction Moisture',g12.5) SPEC RATIO TO 0.45 TOL-SPEC 0.01 VARY BLOCK-VAR BLOCK=S505 SENTENCE=FRAC VARIABLE=FRACS & ID1=MIXED ID2=571B ELEMENT=1 LIMITS 0.000001 0.40 ; ;--------------------------------------------------------------- ; DESIGN SPECS ; DIGESTER (AREA 6000) ;--------------------------------------------------------------- ; DESIGN-SPEC CT-T610 DEFINE SOL625 STREAM-VAR STREAM=625 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WAT625 STREAM-VAR STREAM=625 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; The spec of 0.05 is just a guess -- MR 24 Apr 97 SPEC"SOL625/(SOL625+WAT625)" TO "0.05" TOL-SPEC"0.001" VARY BLOCK-VAR BLOCK=T610 SENTENCE=FRAC VARIABLE=FRAC & ID1=MIXED ID2=625 LIMITS "0.0" "1.0" ; DESIGN-SPEC CT-S614 DEFINE SOL623 STREAM-VAR STREAM=623 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WAT623 STREAM-VAR STREAM=623 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; The spec of 0.30 is just a guess -- MR 24 Apr 97 SPEC"SOL623/(SOL623+WAT623)" TO "0.3" TOL-SPEC"0.001" VARY BLOCK-VAR BLOCK=S614 SENTENCE=FRAC VARIABLE=FRAC & ID1=MIXED ID2=623 LIMITS "0.0" "1.0" ; ;---------------------------------------------------------------- ; BOILER DESIGN-SPECS ;--------------------------------------------------------------- ; DESIGN-SPEC COMBAIR ;CONTROLS THE COMBUSTION AIR FOR A 20% EXCESS DEFINE O2IN MOLE-FLOW STREAM=804E SUBSTREAM=MIXED & COMPONENT=O2 DEFINE O2OUT MOLE-FLOW STREAM=804C SUBSTREAM=MIXED & COMPONENT=O2 DEFINE BNDLOW PARAMETER 55 DEFINE BNDHIH PARAMETER 56 SPEC "O2IN" TO "6.0 * O2OUT" TOL-SPEC "0.01" VARY STREAM-VAR STREAM=804 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS BNDLOW BNDHIH ; LIMITS "250000" "800000" ; ;--------------------------------------------------------------------- ; STEAM CYCLE DESIGN-SPECS ;-------------------------------------------------------------------- ; DESIGN-SPEC DEAERHT ;CONTROLS THE AMOUNT OF MED PRESSURE STEAM ;TO THE DEAERATOR. DEFINE QDEAER INFO-VAR INFO=HEAT VARIABLE=DUTY & STREAM=QDEAER SPEC "QDEAER" TO "0" TOL-SPEC "100" VARY BLOCK-VAR BLOCK=M811ISPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=815A ; VARY BLOCK-VAR BLOCK=M811ISPT SENTENCE=FRAC VARIABLE=FRAC & ; ID1=815A LIMITS 10000 90000 ; DESIGN-SPEC ECONSTM ;CONTROLS THE AMOUNT OF HIGH PRESSURE STEAM TO THE ;ECONOMIZER. DEFINE QECON INFO-VAR INFO=HEAT VARIABLE=DUTY & STREAM=QH811EX SPEC "QECON" TO "0" TOL-SPEC "100" VARY BLOCK-VAR BLOCK=M811HSPT SENTENCE=FRAC VARIABLE=FRAC & ID1=812B LIMITS ".0005" "0.5" ; DESIGN-SPEC SETSTEAM DEFINE QSUPXS INFO-VAR INFO=HEAT VARIABLE=DUTY & STREAM=QM803EX SPEC "QSUPXS" TO "0" TOL-SPEC "100" VARY STREAM-VAR STREAM=824 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "1.0E4" "3.5E5" ; DESIGN-SPEC VLPSTM ;CONTROLS THE AMOUNT OF VERY LOW PRESSURE STEAM ;TO THE EVAPORATOR. DEFINE QEVAP1 INFO-VAR INFO=HEAT VARIABLE=DUTY & STREAM=QE501A DEFINE QEVAP2 INFO-VAR INFO=HEAT VARIABLE=DUTY & STREAM=QE501A2 SPEC "QEVAP2" TO "QEVAP1" TOL-SPEC "0.1" VARY BLOCK-VAR BLOCK=M811LSPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=860 LIMITS 0 500000 ;---------------------------------------------------------------- ; UTILITY DESIGN-SPECS ;----------------------------------------------------------------- ; DESIGN-SPEC CHWFLOW ;CALCULATES THE AMOUNT OF CHILLED WATER REQUIRED TO ;HANDLE THE LOAD FOR THE PLANT. DEFINE QCHW INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QCHILXS SPEC "QCHW" TO "0" TOL-SPEC "50" VARY STREAM-VAR STREAM=950 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "1E4" "8E6" ; DESIGN-SPEC CWFLOWA ;CONTROLS THE COOLING WATER FLOW TO MEET THE DEMAND OF THE ;PLANT. DEFINE QTOT INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QTTOTXS SPEC "QTOT" TO "0" TOL-SPEC "100" VARY STREAM-VAR STREAM=945 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "300000" "30000000" ; DESIGN-SPEC CWFLOWB ;CONTROLS THE COOLING WATER FLOW TO MEET THE DEMAND OF THE ;PLANT (OPERATING COST CALC). DEFINE QTOT INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QTTOTXB SPEC "QTOT" TO "0" TOL-SPEC "100" VARY STREAM-VAR STREAM=946 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "300000" "30000000" ; DESIGN-SPEC CWFLOWC ;CONTROLS THE COOLING WATER FLOW TO MEET THE DEMAND OF THE ;PLANT (EVAPORATION CALC). DEFINE QTOT INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QCWFLXS SPEC "QTOT" TO "0" TOL-SPEC "100" VARY STREAM-VAR STREAM=948 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW LIMITS "10000" "30000000" ; ;------------------------------------------------------- ; *FORTRAN BLOCKS* ; Common Block Holder ;------------------------------------------------------- FORTRAN SETVAR ;F COMMON /CLSSET/ CLYLD, CLPROD, CLVES, CLVOL, CLWV ; Inputs are entered here to be used in common blocks throughout ; the model ; DEFINE SSFVES PARAMETER 31 DEFINE SSFDAY PARAMETER 32 DEFINE SSFVOL PARAMETER 33 DEFINE SSFWV PARAMETER 34 DEFINE PMPSSF PARAMETER 35 ; DEFINE SACVES PARAMETER 36 DEFINE SACDAY PARAMETER 37 DEFINE SACVOL PARAMETER 38 DEFINE SACWV PARAMETER 39 DEFINE PMPSAC PARAMETER 40 ; DEFINE CLYLD PARAMETER 41 DEFINE CLPROD PARAMETER 42 DEFINE CLVOL PARAMETER 44 DEFINE CLWV PARAMETER 45 DEFINE TEMP STREAM-VAR STREAM=101 SUBSTREAM=MIXED & VARIABLE=TEMP ; c FERMENTATION PARAMETERS c SSFDAY is the SSCF residence time in days F SSFDAY=1.5 c SSFVOL is the volume per fermenter of the SSCF vessels in liters F SSFVOL=1000000*3.785 c SSFWV is the working volume to total vol ratio of the SSCF vessels F SSFWV=0.95 ; c SACCHARIFICATION PARAMETERS c SACDAY is the Saccharification residence time in days F SACDAY=1.5 c SACVOL is the volume per tank of the Sacch. vessels in liters F SACVOL=1000000*3.785 c SACWV is the working volume to total vol ratio of the Sacch. vessels F SACWV=0.95 ; c CELLULASE PRODUCTION PARAMETERS c CLYLD is the cellulase yield (FPU/g cellulose + xylose) F CLYLD=200 c CLPROD is the cellulase productivity (FPU/L hr) F CLPROD=75 c CLVOL is the volume per cellulase reactor (L) F CLVOL=264000*3.785 c CLWV is the working volume to total vol ratio of the cell. vsls. F CLWV=0.8 C WRITE-VARS SSFDAY SSFVOL SSFWV SACDAY SACVOL SACWV & CLYLD CLPROD CLVOL CLWV ; EXECUTE FIRST ; ;---------------------------------------------------- ; FEED HANDLING FORTRAN BLOCKS - AREA 100 ;---------------------------------------------------- ; FORTRAN FEEDPROP ; ;THIS BLOCK CALCULATES THE NECESSARY FLOW INFORMATION FOR STRM101 ;GIVEN THE DRY MASS FRACTIONS. ; Higher heating value parameters for SOLSLDS, EXTRACT and PROTEIN ; These values are passed to COMBHEAT DEFINE HCSOL PARAMETER 7 DEFINE HCPRO PARAMETER 8 DEFINE HCEXT PARAMETER 9 ; Lower heating value parameters for SOLSLDS, EXTRACT and PROTEIN ; These values are passed to COMBHET2 DEFINE CMBSOL PARAMETER 10 DEFINE CMBEXT PARAMETER 11 DEFINE CMBPRO PARAMETER 12 ; COD values in (kg O2/kg component) ; These values are passed to CODCALC1, CODCALC2, AND CODEND DEFINE CEXTR PARAMETER 13 DEFINE CPRO PARAMETER 14 DEFINE CSOLS PARAMETER 15 ; Write Variable - Heat of Formation for SOLSLDS, EXTRACT and PROTEIN DEFINE HFSS UNARY-PARAM VARIABLE=DHFORM ID1=SOLSLDS ID2=1 DEFINE HFEXT UNARY-PARAM VARIABLE=DHFORM ID1=EXTRACT ID2=1 DEFINE HFPRO UNARY-PARAM VARIABLE=DHFORM ID1=PROTEIN ID2=1 ; Write Variable - Molecular weight of SOLSLDS, EXTRACT and PROTEIN DEFINE SOLMW UNARY-PARAM VARIABLE=MW ID1=SOLSLDS ID2=1 DEFINE EXTMW UNARY-PARAM VARIABLE=MW ID1=EXTRACT ID2=1 DEFINE PROMW UNARY-PARAM VARIABLE=MW ID1=PROTEIN ID2=1 ; Write Variable - Coefficient for water in block M803CMB for sol solids DEFINE SSH2O BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=27 ID2=MIXED ID3=H2O DEFINE EXTH2O BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=36 ID2=MIXED ID3=H2O DEFINE PROH20 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=37 ID2=MIXED ID3=H2O ; Write Variable - Coefficient for CO2 in block M803CMb for sol solids DEFINE SSCO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=27 ID2=MIXED ID3=CO2 DEFINE EXTCO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=36 ID2=MIXED ID3=CO2 DEFINE PROCO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=37 ID2=MIXED ID3=CO2 ; Write Variable - Coefficient for N2 in block M803CMB for sol solids DEFINE SSN2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=27 ID2=MIXED ID3=N2 DEFINE EXTN2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=36 ID2=MIXED ID3=N2 DEFINE PRON2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=37 ID2=MIXED ID3=N2 ; Write Variable - Coefficient for SO2 in block M803CMB for sol solids DEFINE SSSO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=27 ID2=MIXED ID3=SO2 DEFINE EXTSO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=36 ID2=MIXED ID3=SO2 DEFINE PROSO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=37 ID2=MIXED ID3=SO2 ; Write Variable - Coefficients for O2 in block M803CMB for sol solids DEFINE SSO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=27 ID2=MIXED ID3=O2 DEFINE EXTO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=36 ID2=MIXED ID3=O2 DEFINE PROO2 BLOCK-VAR BLOCK=M803CMB VARIABLE=COEF SENTENCE=STOIC & ID1=37 ID2=MIXED ID3=O2 ; Write Variable - Coefficients for O2 in block T608 for sol solids DEFINE TSSO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=19 ID2=MIXED ID3=O2 DEFINE TEXTO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=47 ID2=MIXED ID3=O2 DEFINE TPROO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=48 ID2=MIXED ID3=O2 ; Write Variable - Coefficients for H2O in block T608 for sol solids DEFINE TSSH2O BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=19 ID2=MIXED ID3=H2O DEFINE TEXH2O BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=47 ID2=MIXED ID3=H2O DEFINE TPRH2O BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=48 ID2=MIXED ID3=H2O ; Write Variable - Coefficients for CO2 in block T608 for sol solids DEFINE TSSCO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=19 ID2=MIXED ID3=CO2 DEFINE TEXCO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=47 ID2=MIXED ID3=CO2 DEFINE TPRCO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=48 ID2=MIXED ID3=CO2 ; Write Variable - Coefficients for NO2 in block T608 for sol solids DEFINE TSSNO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=19 ID2=MIXED ID3=NO2 DEFINE TEXNO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=47 ID2=MIXED ID3=NO2 DEFINE TPRNO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=48 ID2=MIXED ID3=NO2 ; Write Variable - Coefficients for SO2 in block T608 for sol solids DEFINE TSSSO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=19 ID2=MIXED ID3=SO2 DEFINE TEXSO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=47 ID2=MIXED ID3=SO2 DEFINE TPRSO2 BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=48 ID2=MIXED ID3=SO2 ; Write Variable - Coefficients for biomass in block T608 for sol solids DEFINE BIOSS BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=31 ID2=CISOLID ID3=BIOMASS DEFINE BIOEXT BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=49 ID2=CISOLID ID3=BIOMASS DEFINE BIOPRO BLOCK-VAR BLOCK=T608 VARIABLE=COEF SENTENCE=STOIC & ID1=50 ID2=CISOLID ID3=BIOMASS ; Internal variables ; These variables will be directly entered into this fortran block ; Variables: DFEXT - Dry Mass Fraction of Extractives ; DFCELL- Dry Mass Fraction of Cellulose ; DFXYL - Dry Mass Fraction of Xylan ; DFGAL - Dry Mass Fraction of Galactan ; DFARAB- Dry Mass Fraction of Arabinan ; DFMAN - Dry Mass Fraction of Mannan ; DFLIG - Dry Mass Fraction of Lignin ; DFASH - Dry Mass Fraction of Ash ; DFACE - Dry Mass Fraction of Acetate ; DFPRO - Dry Mass Fraction of Protein ; DFSS - Dry Mass Fraction of Soluble Solids ; WET - Percent Moisture in Feedstock ; RATE - Plant feedrate ; CFRAC - Carbon weight fraction ; HFRAC - Hydrogen weight fraction ; OFRAC - Oxygen weight fraction ; FRACN - Nitrogen weight fraction ; SFRAC - Sulfur weight fraction ; AFRAC - Ash weight fraction ; HHVFS - Higher heating value for the feedstock (BTU/LB) ; CLIG - Number of carbon atoms in lignin ; HLIG - Number of hydrogen atoms in lignin ; OLIG - Number of oxygen atoms in lignin ; ACEC - Number of carbon atoms in acetate ; ACEH - Number of hydrogen atoms in acetate ; ACEO - Number of oxygen atoms in acetate ; MWACE - Molecular weight of acetate ; The following variables are internal variables needed for calculations ; C6 - Total dry weight fraction of all carbon six compounds ; C5 - Total dry weight fraction of all carbon five compounds ; SOLS - Total dry weight fraction of all soluble compounds ; CMW - Molecular weight of carbon ; HMW - Molecular weight of hydrogen ; OMW - Molecular weight of oxygen ; NMW - Molecular weight of nitrogen ; SMW - Molecular weight of sulfur ; HFCO2 - Heat of formation of CO2 (J/kmol) ; HFH2O - Heat of formation of H2O (J/kmol) ; HFSO2 - Heat of formation of SO2 (J/kmol) ; HFNO2 - Heat of formation of NO2 (J/kmol) ; HVAP - Water heat of vaporization (J/kmol) ; AFHHV - Ash free higher heating value for the feedstock ; CELLC - Number of carbon atoms in cellulose ; CELLH - Number of hydrogen atoms in cellulose ; CELLO - Number of oxygen atoms in cellulose ; XYLC - Number of carbon atoms in xylan ; XYLH - Number of hydrogen atoms in xylan ; XYLO - Number of oxygen atoms in xylan ; AFEC - Ash free carbon moles from the element analysis ; AFEH - Ash free hydrogen moles from the element analysis ; AFEO - Ash free oxygen moles from the element analysis ; AFEN - Ash free nitrogen moles from the element analysis ; AFES - Ash free sulfur moles from the element analysis ; AFCC - Ash free cellulose moles from the component analysis ; AFCX - Ash free xylan moles from the component analysis ; AFCL - Ash free lignin moles from the component analysis ; AFCA - Ash free acetate moles from the component analysis ; AFCS - Ash free solubles moles from the component analysis ; WAFC - Ash free weight fraction of cellulose ; WAFX - Ash free weight fraction of xylan ; WAFL - Ash free weight fraction of lignin ; WAFA - Ash free weight fraction of acetate ; WAFS - Ash free weight fraction of soluble solids ; CELLMW - Molecular weight of cellulose ; XYLMW - Molecular weight of xylan ; WMLIG - Molecular weight of lignin ; SOLMW - Molecular weight of soluble solids ; EAFC - Excess ash free carbon ; EAFH - Excess ash free hydrogen ; EAFO - Excess ash free oxygen ; EAFN - Excess ash free nitrogen ; EAFS - Excess ash free sulfur ; HCSOL - Higher heating value for soluble solids ; HHVC - Higher heating value of cellulose ; HHVX - Higher heating value of xylan ; HHVL - Higher heating value of lignin ; HHVA - Higher heating value of acetate ; CCO2 - CO2 combustion coefficient ; CH2O - H2O combustion coefficient ; CNO2 - NO2 combustion coefficient ; CSO2 - SO2 combustion coefficient ; CO2 - O2 combustion coefficient ; HFV - Heat of formation for vapor water product ; BIOMW - Molecular weight of biomass ;Values entered by user F DFEXT = 0.0468 F DFCELL = 0.374 F DFXYL = 0.2107 F DFGAL = 0.0194 F DFARAB = 0.0292 F DFMAN = 0.0156 F DFLIG = 0.1799 F DFASH = 0.0523 F DFACE = 0.0293 F DFPRO = 0.031 F DFSS = 0.0112 F WET = 0.15 F RATE = 2000.0 F CFRAC = 0.4452 F HFRAC = 0.0574 F OFRAC = 0.4242 F FRACN = 0.0046 F SFRAC = 0.00008 F AFRAC = 0.0686 F HHVFS = 7503.0 ; May need to be changed if lignin or acetate info changes F CLIG = 10.0 F HLIG = 13.9 F OLIG = 1.3 F ACEC = 2.0 F ACEH = 4.0 F ACEO = 2.0 F ACEMW = 60.05298 F HHVL = 10980.0 F HHVA = 6462.0 ; Internal variables and constants F CMW = 12.011 F HMW = 1.0079 F OMW = 15.9994 F WMN = 14.0067 F SMW = 32.06 F HFCO2 = -393776000.0 F HFH2O = -288043000.0 F HFSO2 = -296840000.0 F HFNO2 = 33180000.0 F HVAP = 4186800.0 F CELLC = 6.0 F CELLH = 10.0 F CELLO = 5.0 F XYLC = 5.0 F XYLH = 8.0 F XYLO = 4.0 F CELLMW = 162.1436 F XYLMW = 132.117 F HHVC = 7464.0 F HHVX = 7645.0 F C6 = DFGAL + DFMAN + DFCELL F C5 = DFXYL + DFARAB F SOLS = DFPRO + DFSS + DFEXT F BIOMW = 23.23747 F AFHHV = HHVFS/(1-AFRAC) F WMLIG = CLIG*CMW + HLIG*HMW + OLIG*OMW ; Calculation of the soluble solids empirical formula F AFEC = (CFRAC/CMW)/(1-AFRAC) F AFEH = (HFRAC/HMW)/(1-AFRAC) F AFEO = (OFRAC/OMW)/(1-AFRAC) F AFEN = (FRACN/WMN)/(1-AFRAC) F AFES = (SFRAC/SMW)/(1-AFRAC) F WRITE(NHSTRY,*)'Ultimate: Ash Free Carbon= ',AFEC F WAFC = C6/(1-DFASH) F WAFX = C5/(1-DFASH) F WAFL = DFLIG/(1-DFASH) F WAFA = DFACE/(1-DFASH) F WAFS = SOLS/(1-DFASH) F AFCC = WAFC/CELLMW F AFCX = WAFX/XYLMW F AFCL = WAFL/WMLIG F AFCA = WAFA/ACEMW F AFCS = 1-AFCC-AFCX-AFCL-AFCA F EAFC = AFEC - AFCC*CELLC-AFCX*XYLC-AFCL*CLIG-AFCA*ACEC F EAFH = AFEH - AFCC*CELLH-AFCX*XYLH-AFCL*HLIG-AFCA*ACEH F EAFO = AFEO - AFCC*CELLO-AFCX*XYLO-AFCL*OLIG-AFCA*ACEO F EAFN = AFEN F EAFS = AFES F SSC = EAFC/EAFC F SSH = EAFH/EAFC F SSO = EAFO/EAFC F SSN = EAFN/EAFC F SSS = EAFS/EAFC F WRITE (NHSTRY,*) 'FEEDPROP Atomic Numbers:' F WRITE (NHSTRY,*) 'C,H,O,N,S:',SSC, SSH, SSO, SSN, SSS F EXTC = SSC F PROC = SSC F EXTH = SSH F PROH = SSH F EXTO = SSO F PROO = SSO F EXTN = SSN F PRON = SSN F EXTS = SSS F PROS = SSS F SOLMW = SSC*CMW + SSH*HMW + SSO*OMW + SSN*WMN + SSS*SMW F EXTMW = SOLMW F PROMW = SOLMW F WRITE (NHSTRY,*) 'FEEDPROP Molecular Weights:' F WRITE(NHSTRY,*)'SOLS,PROT,EXTR= ', SOLMW, PROMW, EXTMW ; Reaction stoichiometry for block M803CMB F SSH2O = SSH/2.0 F EXTH2O = SSH2O F PROH2O = SSH2O F SSCO2 = SSC F EXTCO2 = SSCO2 F PROCO2 = SSCO2 F SSN2 = SSN/2.0 F EXTN2 = SSN2 F PRON2 = SSN2 F SSSO2 = SSS F EXTSO2 = SSS F PROSO2 = SSS F SSO2 = (SSO - SSH2O - SSCO2*2.0 - SSSO2*2.0)/2.0 F EXTO2 = SSO2 F PROO2 = SSO2 F WRITE (NHSTRY,*) 'FEEDPROP Combustion Stoichiometry - M803CMB' F WRITE (NHSTRY,*) 'SSH2O,SSCO2,SSN2,SSSO2,SSO2:', F 1 SSH2O, SSCO2, SSN2, SSSO2, SSO2 ; Calculates higher heating value for the soluble solids (btu/kg) F HCSOL=AFHHV-(C6*HHVC+C5*HHVX+DFLIG*HHVL+DFACE*HHVA)/(1-DFASH) F HCSOL = HCSOL/(SOLS/(1-DFASH))*2.20462 F HCPRO = HCSOL F HCEXT = HCSOL F WRITE(NHSTRY,*)'HCSOL= ',HCSOL ; Combustion stoichiometry calculations F CCO2 = SSC F CH2O = SSH/2.0 F CNO2 = SSN F CSO2 = SSS F CO2 = (SSO-CCO2*2.0-CH2O-CNO2*2.0-CSO2*2.0)/2.0 ; These are used in T608 reactions F TSSO2 = CO2 F TEXTO2 = CO2 F TPROO2 = CO2 F TSSH2O = CH2O F TEXH2O = CH2O F TPRH2O = CH2O F TSSCO2 = CCO2 F TEXCO2 = CCO2 F TPRCO2 = CCO2 F TSSNO2 = CNO2 F TEXNO2 = CNO2 F TPRNO2 = CNO2 F TSSSO2 = CSO2 F TEXSO2 = CSO2 F TPRSO2 = CSO2 ; Heat of formation calculations for liquid water product (J/kmol) F HFSS=-(-HCSOL*SOLMW*1055.1) F HFSS=HFSS-(-(HFCO2*CCO2+HFH2O*CH2O+HFNO2*CNO2+HFSO2*CSO2)) F HFEXT = HFSS F HFPRO = HFSS F WRITE(NHSTRY,*)'HFSS= ',HFSS ; Heat of formation calculations for vapor water product (J/kmol) F HFV = HFSS - CH2O*HVAP F WRITE(NHSTRY,*)'HFV= ',HFV ; Calculates lower heating value for the soluble solids (J/kmol) F CMBSOL = (HFCO2*CCO2+HFH2O*CH2O+HFSO2*CSO2+HFNO2*CNO2)-HFV F CMBEXT = CMBSOL F CMBPRO = CMBSOL F WRITE(NHSTRY,*)'CMBSOL= ',CMBSOL ; Calculation of COD values ; If CO2 is positive, COD contribution from CEXTR, etc. should be 0. ; If CO2 is negative, COD contribution from CEXTR, etc. should be +. F IF (CO2.LT.0) THEN F CEXTR = -(CO2*OMW*2.0)/SOLMW F ELSE F CEXTR=0.0 F END IF F CPRO = CEXTR F CSOLS = CEXTR F WRITE(NHSTRY,*)'CEXTR= ',CEXTR ; Calculation of BIOMASS coefficients for T608 rxns 31, 49, 50 F BIOSS = SOLMW/BIOMW F BIOEXT = BIOSS F BIOPRO = BIOSS EXECUTE AFTER SETVAR FORTRAN FEEDSTK ; WRITE Variable - Mass Flow of Extractives DEFINE EXTFLO MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=EXTRACT ; WRITE Variable - Mass Flow of Cellulose DEFINE CELLF MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=CELLULOS ; WRITE Variable - Mass Flow of Xylan DEFINE XYLF MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=XYLAN ; WRITE Variable - Mass Flow of Galactan DEFINE GALF MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=GALACTAN ; WRITE Variable - Mass Flow of Arabinan DEFINE ARBF MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=ARABINAN ; WRITE Variable - Mass Flow of Mannan DEFINE FMAN MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=MANNAN ; WRITE Variable - Mass Flow of Lignin DEFINE FLIG MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=LIGNIN ; WRITE Variable - Mass Flow of Ash DEFINE ASHF MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=ASH ; WRITE Variable - Mass Flow of Acetate DEFINE ACETF MASS-FLOW STREAM=101 SUBSTREAM=CISOLID & COMPONENT=ACETATE ; WRITE Variable - Mass Flow of Protein DEFINE PROFLO MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; WRITE Variable - Mass Flow of Soluble Solids DEFINE SSFLO MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=SOLSLDS ; WRITE Variable - Mass Flow of Water DEFINE H2OFLO MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=H2O ; WRITE Variable - Mass Flow of the CISOLID substream in kg/Hr DEFINE CIFLO STREAM-VAR STREAM=101 SUBSTREAM=CISOLID & VARIABLE = MASS-FLOW ; ; Values entered by user F DFEXT = 0.0468 F DFCELL = 0.374 F DFXYL = 0.2107 F DFGAL = 0.0194 F DFARAB = 0.0292 F DFMAN = 0.0156 F DFLIG = 0.1799 F DFASH = 0.0523 F DFACE = 0.0293 F DFPRO = 0.031 F DFSS = 0.0112 F WET = 0.15 F RATE = 2000.0 ; Calculation of Mixed Substream Flowrates (kg/Hr) F H2OFLO = RATE * (1000.0/24.0) * (WET/(1-WET)) F SSFLO = RATE * (1000.0/24.0) * DFSS F EXTFLO = RATE * (1000.0/24.0) * DFEXT F PROFLO = RATE * (1000.0/24.0) * DFPRO F WRITE(NHSTRY,*)'Soluble Solids Flow= ', SSFLO F WRITE(NHSTRY,*)'PROTEIN FLOW =', PROFLO F WRITE(NHSTRY,*)'EXTRACT FLOW =', EXTFLO ; Calculation of CISOLID Substream Flowrate (kg/Hr) F CIFLO = RATE*(1000.0/24.0) - (SSFLO+EXTFLO+PROFLO) ;Calculation of CISOLID Substream Component Mass Fractions F TOT = DFCELL+DFXYL+DFGAL+DFARAB+DFMAN+DFLIG+DFASH+DFACE F CELLF = (DFCELL / TOT) * CIFLO F WRITE(NHSTRY,*)'CELLF= ',CELLF F XYLF = (DFXYL / TOT) * CIFLO F WRITE(NHSTRY,*)'XYLF= ',XYLF F ARBF = (DFARAB / TOT) * CIFLO F WRITE(NHSTRY,*)'ARBF= ',ARBF F FMAN = (DFMAN / TOT) * CIFLO F WRITE(NHSTRY,*)'FMAN= ',FMAN F GALF = (DFGAL / TOT) * CIFLO F WRITE(NHSTRY,*)'GALF= ',GALF F FLIG = (DFLIG / TOT) * CIFLO F WRITE(NHSTRY,*)'FLIG= ',FLIG F ACETF = (DFACE / TOT) * CIFLO F WRITE(NHSTRY,*)'ACETF= ',ACETF F ASHF = (DFASH / TOT) * CIFLO F WRITE(NHSTRY,*)'ASHF= ',ASHF EXECUTE AFTER FEEDPROP ; FORTRAN POLY1 DEFINE POLY STREAM-VAR STREAM=107 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE FEEDMX STREAM-VAR STREAM=101 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE FEEDSL STREAM-VAR STREAM=101 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW c c POLREQ is the polymer requirement (ppm) as function of feed to clarifier. c The feed to clarifier is 5000 gpm per Harris 2000 subcontract report c so CLARFD is set at 5000 gpm * 3.785 L/gal * 1 kg/L * 60 min/hr (so it c is in units kg/hr and is ratioed off of stream 101 -- 98040 kg/hr total c in Harris subcontract). F POLREQ = 25.0 F CLARFD = 5000.0 * 3.785 * 1.0 * 60.0 * ((FEEDMX+FEEDSL)/98040.0) C F POLY = POLREQ * CLARFD / 1000000.0 C READ-VARS FEEDMX FEEDSL WRITE-VARS POLY ; ;---------------------------------------------------- ; PRETREATMENT FORTRAN BLOCKS - AREA 200 ;---------------------------------------------------- ; FORTRAN S205WASH DEFINE SOL220 STREAM-VAR STREAM=220 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW DEFINE WAT220 STREAM-VAR STREAM=220 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE WSH252 BLOCK-VAR BLOCK=S205SPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=252 DEFINE AIRRQ STREAM-VAR STREAM=257 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW ; F WASHR2 = 0.58 F WSH252 = WASHR2 * (SOL220 + WAT220) C ; calculation of air requirement ; airflw = required flow in CFM ; airp = pressure of airflw (psig) ; airt = temperature of airflw (C) F AIRFLW = 2 * 1180.0 F AIRP = 0.0 F AIRT = 25.0 F AIRNUM = ((AIRP+14.6096)*100000.0/14.5038*AIRFLW/35.3147) F AIRDEN = (8.314 * (AIRT + 273.15)) ; conversion of AIRRQ to kmol/hr F AIRRQ = (AIRNUM/AIRDEN) / 1000.0 * 60.0 F WRITE(NHSTRY,*)'AIRNUM IN 257= ',AIRNUM F WRITE(NHSTRY,*)'AIRDEN IN 257= ',AIRDEN F WRITE(NHSTRY,*)'MOLEFLOW IN 257= ',AIRRQ READ-VARS SOL220 WAT220 WRITE-VARS WSH252 AIRRQ ; FORTRAN S205SOL ; DEFINE FS1 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & ; VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=1 ; Water set by CT-S205B to get proper insol solids DEFINE FS2 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=2 ; Calculate the recovery ; The mean solubles removal efficiency is 93.3% according to ; Pneumapress P100 Test (#9) (Under Harris 2000 Subcontract) ; That removal includes both concentrated recovery stream (221) & ; dilute recovery stream (256). This Fort. Block calculates the ; recovery in the dilute stream to hit the desired overall recovery ; for xylose and sets all solubles to same recovery F RECOV=0.933 DEFINE ETH220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE ETH221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE ETH254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE ETH252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=ETHANOL F IF (ETH254.GT.0) THEN F FS2 = ((RECOV * ETH220) - ETH221 + ETH252) / ETH254 F ELSE F FS2 = 0.0 F ENDIF F WRITE(NHSTRY,*)'ETHANOL RECOVERY IN S205B= ',FS2 DEFINE FS3 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=3 DEFINE FRF220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=FURFURAL DEFINE FRF221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=FURFURAL DEFINE FRF254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=FURFURAL DEFINE FRF252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=FURFURAL F IF (FRF254.GT.0) THEN F FS3 = ((RECOV * FRF220) - FRF221 + FRF252) / FRF254 F ELSE F FS3 = 0.0 F ENDIF F WRITE(NHSTRY,*)'FURFURAL RECOVERY IN S205B= ',FS3 DEFINE FS4 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=4 DEFINE HMF220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=HMF DEFINE HMF221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=HMF DEFINE HMF254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=HMF DEFINE HMF252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=HMF F IF (HMF254.GT.0) THEN F FS4 = ((RECOV * HMF220) - HMF221 + HMF252) / HMF254 F ELSE F FS4 = 0.0 F ENDIF F WRITE(NHSTRY,*)'HMF RECOVERY IN S205B= ',FS4 DEFINE FS5 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=5 DEFINE H2S220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=H2SO4 DEFINE H2S221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=H2SO4 DEFINE H2S254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=H2SO4 DEFINE H2S252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=H2SO4 F IF (H2S254.GT.0) THEN F FS5 = ((RECOV * H2S220) - H2S221 + H2S252) / H2S254 F ELSE F FS5 = 0.0 F ENDIF F WRITE(NHSTRY,*)'H2SO4 RECOVERY IN S205B= ',FS5 DEFINE FS6 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=6 DEFINE GN2220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=N2 DEFINE GN2221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=N2 DEFINE GN2254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=N2 DEFINE GN2252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=N2 F IF (GN2254.GT.0) THEN F FS6 = ((RECOV * GN2220) - GN2221 + GN2252) / GN2254 F ELSE F FS6 = 0.0 F ENDIF F WRITE(NHSTRY,*)'N2 RECOVERY IN S205B= ',FS6 DEFINE FS7 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=7 DEFINE CO2220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=CO2 DEFINE CO2221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=CO2 DEFINE CO2254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=CO2 DEFINE CO2252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=CO2 F IF (CO2254.GT.0) THEN F FS7 = ((RECOV * CO2220) - CO2221 + CO2252) / CO2254 F ELSE F FS7 = 0.0 F ENDIF F WRITE(NHSTRY,*)'CO2 RECOVERY IN S205B= ',FS7 DEFINE FS8 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=8 DEFINE O2G220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=O2 DEFINE O2G221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=O2 DEFINE O2G254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=O2 DEFINE O2G252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=O2 F IF (O2G254.GT.0) THEN F FS8 = ((RECOV * O2G220) - O2G221 + O2G252) / O2G254 F ELSE F FS8 = 0.0 F ENDIF F WRITE(NHSTRY,*)'O2 RECOVERY IN S205B= ',FS8 DEFINE FS9 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=9 DEFINE CH4220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=CH4 DEFINE CH4221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=CH4 DEFINE CH4254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=CH4 DEFINE CH4252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=CH4 F IF (CH4254.GT.0) THEN F FS9 = ((RECOV * CH4220) - CH4221 + CH4252) / CH4254 F ELSE F FS9 = 0.0 F ENDIF F WRITE(NHSTRY,*)'CH4 RECOVERY IN S205B= ',FS9 DEFINE FS10 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=10 DEFINE GNO220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=NO DEFINE GNO221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=NO DEFINE GNO254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=NO DEFINE GNO252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=NO F IF (GNO254.GT.0) THEN F FS10 = ((RECOV * GNO220) - GNO221 + GNO252) / GNO254 F ELSE F FS10 = 0.0 F ENDIF F WRITE(NHSTRY,*)'NO RECOVERY IN S205B= ',FS10 DEFINE FS11 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=11 DEFINE XNO220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=NO2 DEFINE XNO221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=NO2 DEFINE XNO254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=NO2 DEFINE XNO252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=NO2 F IF (XNO254.GT.0) THEN F FS11 = ((RECOV * XNO220) - XNO221 + XNO252) / XNO254 F ELSE F FS11 = 0.0 F ENDIF F WRITE(NHSTRY,*)'NO2 RECOVERY IN S205B= ',FS11 DEFINE FS12 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=12 DEFINE XNH220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE XNH221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE XNH254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE XNH252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=NH3 F IF (XNH254.GT.0) THEN F FS12 = ((RECOV * XNH220) - XNH221 + XNH252) / XNH254 F ELSE F FS12 = 0.0 F ENDIF F WRITE(NHSTRY,*)'NH3 RECOVERY IN S205B= ',FS12 DEFINE FS13 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=13 DEFINE SOL220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE SOL221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE SOL254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE SOL252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=SOLSLDS F IF (SOL254.GT.0) THEN F FS13 = ((RECOV * SOL220) - SOL221 + SOL252) / SOL254 F ELSE F FS13 = 0.0 F ENDIF F WRITE(NHSTRY,*)'SOLSLDS RECOVERY IN S205B= ',FS13 DEFINE FS14 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=14 DEFINE GLU220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE GLU221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE GLU254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE GLU252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=GLUCOSE F IF (GLU254.GT.0) THEN F FS14 = ((RECOV * GLU220) - GLU221 + GLU252) / GLU254 F ELSE F FS14 = 0.0 F ENDIF F WRITE(NHSTRY,*)'GLUCOSE RECOVERY IN S205B= ',FS14 DEFINE FS15 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=15 DEFINE XYL220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE XYL221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE XYL254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE XYL252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=XYLOSE F IF (XYL254.GT.0) THEN F FS15 = ((RECOV * XYL220) - XYL221 + XYL252) / XYL254 F ELSE F FS15 = 0.0 F ENDIF F WRITE(NHSTRY,*)'XYLOSE RECOVERY IN S205B= ',FS15 DEFINE FS16 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=16 DEFINE GAL220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE GAL221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE GAL254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE GAL252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=GALACTOS F IF (GAL254.GT.0) THEN F FS16 = ((RECOV * GAL220) - GAL221 + GAL252) / GAL254 F ELSE F FS16 = 0.0 F ENDIF F WRITE(NHSTRY,*)'GALACTOSE RECOVERY IN S205B= ',FS16 DEFINE FS17 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=17 DEFINE XMN220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE XMN221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE XMN254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE XMN252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=MANNOSE F IF (XMN254.GT.0) THEN F FS17 = ((RECOV * XMN220) - XMN221 + XMN252) / XMN254 F ELSE F FS17 = 0.0 F ENDIF F WRITE(NHSTRY,*)'MANNOSE RECOVERY IN S205B= ',FS17 DEFINE FS18 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=18 DEFINE ARA220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE ARA221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE ARA254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE ARA252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=ARABINOS F IF (ARA254.GT.0) THEN F FS18 = ((RECOV * ARA220) - ARA221 + ARA252) / ARA254 F ELSE F FS18 = 0.0 F ENDIF F WRITE(NHSTRY,*)'ARABINOSE RECOVERY IN S205B= ',FS18 DEFINE FS19 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=19 DEFINE UNK220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=UNKNOWN DEFINE UNK221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=UNKNOWN DEFINE UNK254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=UNKNOWN DEFINE UNK252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=UNKNOWN F IF (UNK254.GT.0) THEN F FS19 = ((RECOV * UNK220) - UNK221 + UNK252) / UNK254 F ELSE F FS19 = 0.0 F ENDIF F WRITE(NHSTRY,*)'UNKNOWN RECOVERY IN S205B= ',FS19 DEFINE FS20 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=20 DEFINE AAC220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=AACID DEFINE AAC221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=AACID DEFINE AAC254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=AACID DEFINE AAC252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=AACID F IF (AAC254.GT.0) THEN F FS20 = ((RECOV * AAC220) - AAC221 + AAC252) / AAC254 F ELSE F FS20 = 0.0 F ENDIF F WRITE(NHSTRY,*)'AACID RECOVERY IN S205B= ',FS20 DEFINE FS21 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=21 DEFINE LAC220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=LACID DEFINE LAC221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=LACID DEFINE LAC254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=LACID DEFINE LAC252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=LACID F IF (LAC254.GT.0) THEN F FS21 = ((RECOV * LAC220) - LAC221 + LAC252) / LAC254 F ELSE F FS21 = 0.0 F ENDIF F WRITE(NHSTRY,*)'LACID RECOVERY IN S205B= ',FS21 DEFINE FS22 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=22 DEFINE CNU220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE CNU221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE CNU254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE CNU252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=CNUTR F IF (CNU254.GT.0) THEN F FS22 = ((RECOV * CNU220) - CNU221 + CNU252) / CNU254 F ELSE F FS22 = 0.0 F ENDIF F WRITE(NHSTRY,*)'CNUTR RECOVERY IN S205B= ',FS22 DEFINE FS23 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=23 DEFINE WNU220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE WNU221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE WNU254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE WNU252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=WNUTR F IF (WNU254.GT.0) THEN F FS23 = ((RECOV * WNU220) - WNU221 + WNU252) / WNU254 F ELSE F FS23 = 0.0 F ENDIF F WRITE(NHSTRY,*)'WNUTR RECOVERY IN S205B= ',FS23 DEFINE FS24 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=24 DEFINE CSL220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE CSL221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE CSL254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE CSL252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=CSL F IF (CSL254.GT.0) THEN F FS24 = ((RECOV * CSL220) - CSL221 + CSL252) / CSL254 F ELSE F FS24 = 0.0 F ENDIF F WRITE(NHSTRY,*)'CSL RECOVERY IN S205B= ',FS24 DEFINE FS25 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=25 DEFINE OIL220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=OIL DEFINE OIL221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=OIL DEFINE OIL254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=OIL DEFINE OIL252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=OIL F IF (OIL254.GT.0) THEN F FS25 = ((RECOV * OIL220) - OIL221 + OIL252) / OIL254 F ELSE F FS25 = 0.0 F ENDIF F WRITE(NHSTRY,*)'OIL RECOVERY IN S205B= ',FS25 DEFINE FS26 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=26 DEFINE DEN220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=DENAT DEFINE DEN221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=DENAT DEFINE DEN254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=DENAT DEFINE DEN252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=DENAT F IF (DEN254.GT.0) THEN F FS26 = ((RECOV * DEN220) - DEN221 + DEN252) / DEN254 F ELSE F FS26 = 0.0 F ENDIF F WRITE(NHSTRY,*)'DENAT RECOVERY IN S205B= ',FS26 DEFINE FS27 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=27 DEFINE GLG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE GLG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE GLG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE GLG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG F IF (GLG254.GT.0) THEN F FS27 = ((RECOV * GLG220) - GLG221 + GLG252) / GLG254 F ELSE F FS27 = 0.0 F ENDIF F WRITE(NHSTRY,*)'GLUCOLIG RECOVERY IN S205B= ',FS27 DEFINE FS28 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=28 DEFINE CLB220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE CLB221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE CLB254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE CLB252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=CELLOB F IF (CLB254.GT.0) THEN F FS28 = ((RECOV * CLB220) - CLB221 + CLB252) / CLB254 F ELSE F FS28 = 0.0 F ENDIF F WRITE(NHSTRY,*)'CELLOB RECOVERY IN S205B= ',FS28 DEFINE FS29 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=29 DEFINE XLG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE XLG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE XLG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE XLG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=XYLOLIG F IF (XLG254.GT.0) THEN F FS29 = ((RECOV * XLG220) - XLG221 + XLG252) / XLG254 F ELSE F FS29 = 0.0 F ENDIF F WRITE(NHSTRY,*)'XYLOLIG RECOVERY IN S205B= ',FS29 DEFINE FS30 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=30 DEFINE ZLG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE ZLG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE ZLG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE ZLG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=MANOLIG F IF (ZLG254.GT.0) THEN F FS30 = ((RECOV * ZLG220) - ZLG221 + ZLG252) / ZLG254 F ELSE F FS30 = 0.0 F ENDIF F WRITE(NHSTRY,*)'MANOLIG RECOVERY IN S205B= ',FS30 DEFINE FS31 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=31 DEFINE GGG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE GGG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE GGG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE GGG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=GALAOLIG F IF (GGG254.GT.0) THEN F FS31 = ((RECOV * GGG220) - GGG221 + GGG252) / GGG254 F ELSE F FS31 = 0.0 F ENDIF F WRITE(NHSTRY,*)'GALAOLIG RECOVERY IN S205B= ',FS31 DEFINE FS32 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=32 DEFINE ARG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE ARG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE ARG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE ARG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=ARABOLIG F IF (ARG254.GT.0) THEN F FS32 = ((RECOV * ARG220) - ARG221 + ARG252) / ARG254 F ELSE F FS32 = 0.0 F ENDIF F WRITE(NHSTRY,*)'ARABOLIG RECOVERY IN S205B= ',FS32 DEFINE FS33 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=33 DEFINE ACG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE ACG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE ACG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE ACG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=ACETOLIG F IF (ACG254.GT.0) THEN F FS33 = ((RECOV * ACG220) - ACG221 + ACG252) / ACG254 F ELSE F FS33 = 0.0 F ENDIF F WRITE(NHSTRY,*)'ACETOLIG RECOVERY IN S205B= ',FS33 DEFINE FS34 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=34 DEFINE GLY220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=GLYCEROL DEFINE GLY221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=GLYCEROL DEFINE GLY254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=GLYCEROL DEFINE GLY252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=GLYCEROL F IF (GLY254.GT.0) THEN F FS34 = ((RECOV * GLY220) - GLY221 + GLY252) / GLY254 F ELSE F FS34 = 0.0 F ENDIF F WRITE(NHSTRY,*)'GLYCEROL RECOVERY IN S205B= ',FS34 DEFINE FS35 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=35 DEFINE SUC220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=SUCCACID DEFINE SUC221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=SUCCACID DEFINE SUC254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=SUCCACID DEFINE SUC252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=SUCCACID F IF (SUC254.GT.0) THEN F FS35 = ((RECOV * SUC220) - SUC221 + SUC252) / SUC254 F ELSE F FS35 = 0.0 F ENDIF F WRITE(NHSTRY,*)'SUCCACID RECOVERY IN S205B= ',FS35 DEFINE FS36 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=36 DEFINE XYT220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=XYLITOL DEFINE XYT221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=XYLITOL DEFINE XYT254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=XYLITOL DEFINE XYT252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=XYLITOL F IF (XYT254.GT.0) THEN F FS36 = ((RECOV * XYT220) - XYT221 + XYT252) / XYT254 F ELSE F FS36 = 0.0 F ENDIF F WRITE(NHSTRY,*)'XYLITOL RECOVERY IN S205B= ',FS36 DEFINE FS37 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=37 DEFINE SLG220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE SLG221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE SLG254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE SLG252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=LGNSOL F IF (SLG254.GT.0) THEN F FS37 = ((RECOV * SLG220) - SLG221 + SLG252) / SLG254 F ELSE F FS37 = 0.0 F ENDIF F WRITE(NHSTRY,*)'LGNSOL RECOVERY IN S205B= ',FS37 DEFINE FS38 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=38 DEFINE EXT220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE EXT221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE EXT254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE EXT252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=EXTRACT F IF (EXT254.GT.0) THEN F FS38 = ((RECOV * EXT220) - EXT221 + EXT252) / EXT254 F ELSE F FS38 = 0.0 F ENDIF F WRITE(NHSTRY,*)'EXTRACT RECOVERY IN S205B= ',FS38 DEFINE FS39 BLOCK-VAR BLOCK=S205B SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=256 ELEMENT=39 DEFINE PRO220 MASS-FLOW STREAM=220 SUBSTREAM=MIXED & COMPONENT=PROTEIN DEFINE PRO221 MASS-FLOW STREAM=221 SUBSTREAM=MIXED & COMPONENT=PROTEIN DEFINE PRO254 MASS-FLOW STREAM=254 SUBSTREAM=MIXED & COMPONENT=PROTEIN DEFINE PRO252 MASS-FLOW STREAM=252 SUBSTREAM=MIXED & COMPONENT=PROTEIN F IF (PRO254.GT.0) THEN F FS39 = ((RECOV * PRO220) - PRO221 + PRO252) / PRO254 F ELSE F FS39 = 0.0 F ENDIF F WRITE(NHSTRY,*)'PROTEIN RECOVERY IN S205B= ',FS39 READ-VARS ETH220 ETH221 ETH254 ETH252 & XYL220 XYL221 XYL254 XYL252 WRITE-VARS FS2 FS3 FS4 FS5 & FS6 FS7 FS8 FS9 FS10 & FS11 FS12 FS13 FS14 FS15 & FS16 FS17 FS18 FS19 FS20 & FS21 FS22 FS23 FS24 FS25 & FS26 FS27 FS28 FS29 FS30 & FS31 FS32 FS33 FS34 FS35 & FS36 FS37 FS38 FS39 ; EXECUTE BEFORE BLOCK S205B ; FORTRAN OLIME DEFINE FL240 STREAM-VAR STREAM=240 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FL227 STREAM-VAR STREAM=227 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW F WM227=74.09 DEFINE FA240 MOLE-FLOW STREAM=240 SUBSTREAM=MIXED COMPONENT=H2SO4 ; FACTOR = THE LIME ADDITION FACTOR (g CaOH / g Hydrolysate Liquor) ; FACTOR = 0.003 was experimentally determined by MN, MA, & TKH on ; P961008SD, P961010SD, and P961014SD, respectively. ; Reduced by factor of 2 due to increased flow with S/L was before IX F FACTOR = 0.01/3 F FL227 = FACTOR * FL240 + FA240 * WM227 EXECUTE BEFORE BLOCK T209 ; FORTRAN REACID DEFINE CA228 MOLE-FLOW STREAM=228 SUBSTREAM=CISOLID COMPONENT=CAH2O2 DEFINE HS228 MOLE-FLOW STREAM=228 SUBSTREAM=MIXED COMPONENT=H2SO4 DEFINE FL233 STREAM-VAR STREAM=233 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW F FL233=CA228-HS228 F IF (FL233.LT.0) FL233=0 EXECUTE BEFORE BLOCK T224 ; ;---------------------------------------------------------------------- ; SSCF FORTRAN BLOCKS - AREA 300 ;---------------------------------------------------------------------- ; FORTRAN FERMCSL ; THIS FORTRAN BLOCK SETS THE CSL FLOWS TO SSCF PRODUCTION AND SEED ; ; INPUTS DEFINE FL303A STREAM-VAR STREAM=303A SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FS303A STREAM-VAR STREAM=303A SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE FL304A STREAM-VAR STREAM=304A SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FS304A STREAM-VAR STREAM=304A SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW ; OUTPUTS DEFINE FL310A MASS-FLOW STREAM=310A SUBSTREAM=MIXED & COMPONENT=CSL DEFINE FL311A MASS-FLOW STREAM=311A SUBSTREAM=MIXED & COMPONENT=CSL ; CSLSD IS THE CSL CONCENTRATION IN THE SEED FERMS (MASS/MASS) F CSLSD=0.005 ; CSLPRD IS THE CSL CONCENTRATION IN THE PRODUCTION FERMS (MASS/MASS) F CSLPRD=0.0025 F FL310A=CSLSD*(FL303A+FS303A) F FL311A=CSLPRD*(FL304A+FS304A) EXECUTE AFTER T310 ; FORTRAN FERMDAP ; THIS FORTRAN BLOCK SETS THE DAP FLOWS TO SSCF PRODUCTION AND SEED ; ; INPUTS DEFINE FM303A STREAM-VAR STREAM=303A SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FC303A STREAM-VAR STREAM=303A SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE DM303A STREAM-VAR STREAM=303A SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE DC303A STREAM-VAR STREAM=303A SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE FM304A STREAM-VAR STREAM=304A SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FC304A STREAM-VAR STREAM=304A SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE DM304A STREAM-VAR STREAM=304A SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE DC304A STREAM-VAR STREAM=304A SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY ; OUTPUTS DEFINE FL310 MASS-FLOW STREAM=310 SUBSTREAM=MIXED & COMPONENT=DAP DEFINE FL311 MASS-FLOW STREAM=311 SUBSTREAM=MIXED & COMPONENT=DAP ; DAPSD IS THE DAP CONCENTRATION IN THE SEED FERMS (MASS/VOLUME) ; DAPPRD IS THE DAP CONC. IN THE PRODUCTION FERMS (MASS/VOLUME) ; DAP nutrient addition rate set at 0.33 g/L; AA 02/16/01 ; VOLFLW1 is the volumetric flow of 303A (L/hr) ; VOLFLW2 is the volumetric flow of 304A (L/hr) F DAPSD=0.67 F DAPPRD=0.33 F VLFLW1 = (FM303A/DM303A + FC303A/DC303A) F VLFLW2 = (FM304A/DM304A + FC304A/DC304A) ; F FL310=(DAPSD/1000)*VLFLW1 F FL311=(DAPPRD/1000)*VLFLW2 F WRITE(NHSTRY,*)'Flow of 303A mixed is ',FM303A,' kg/hr' F WRITE(NHSTRY,*)'Flow of 303A cisolid is ',FC303A,' kg/hr' F WRITE(NHSTRY,*)'Flow of 304A mixed is ',FM304A,' kg/hr' F WRITE(NHSTRY,*)'Flow of 304A cisolid is ',FC304A,' kg/hr' F WRITE(NHSTRY,*)'Density of 303A mixed is ',DM303A,' g/cm3' F WRITE(NHSTRY,*)'Density of 303A cisolid is ',DC303A,' g/cm3' F WRITE(NHSTRY,*)'Density of 304A mixed is ',DM304A,' g/cm3' F WRITE(NHSTRY,*)'Density of 304A cisolid is ',DC304A,' g/cm3' F WRITE(NHSTRY,*)'VLFLW1 = ',VLFLW1,' L/hr' F WRITE(NHSTRY,*)'VLFLW2 = ',VLFLW2,' L/hr' F WRITE(NHSTRY,*)'FL310 = ',FL310,' kg/hr' F WRITE(NHSTRY,*)'FL311 = ',FL311,' kg/hr' ; READ-VARS FM303A FC303A FM304A FC304A & ; DM303A DC303A DM304A DC304A ; WRITE-VARS FL310 FL311 EXECUTE AFTER FERMCSL FORTRAN ENZ2 c MADE CHANGES (*) FOR A SEPARATE SACCHARIFICATION AND FERMENTATION MODE c KI, 3/10/02 c *Cellulase is calculated for whole stream entering Area 300, stream 301A ; DEFINE CL304 MASS-FLOW STREAM=304 SUBSTREAM=CISOLID & ; COMPONENT=CELLULOS DEFINE CL301A MASS-FLOW STREAM=301A SUBSTREAM=CISOLID & COMPONENT=CELLULOS DEFINE XM312 STREAM-VAR STREAM=312 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CI312 STREAM-VAR STREAM=312 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW C ELOAD IS ENZYME LOADING (FPU / G CELLULOSE) F ELOAD = 12.0 C ECONC IS ENZYME CONCENTRATION (50 FPU/ML IS APPROX CURRENT IOGEN CONC F ECONC = 50.0 C ERAT IS ENZYME RATIO (SOLID ENZYME TO WATER) F ERAT = CI312 / (CI312 + XM312) C EREQ IS ENZYME REQUIRED (FPU / HR) F EREQ = ELOAD * 1000 * (CL301A) C DENS IS THE ASSUMED DENSITY OF THE ENZYME (1.000 USED BECAUSE WE ARE ONLY C MODELING ENZYME PROTEIN AND WATER; NO CELL MASS OR PRESERVATIVE) (G/ML) F DENS = 1.0 C EREQM IS THE ENZYME REQUIRED (KG / HR) F EREQM = EREQ / ECONC * DENS / 1000 F CI312 = ERAT * EREQM F XM312 = (1-ERAT) * EREQM READ-VARS CL301A WRITE-VARS XM312 CI312 ; ; ;FORTRAN ENZ2S c MADE CHANGES (*) FOR A SEPARATE SACCHARIFICATION AND FERMENTATION MODE c KI, 3/10/02 c *Removed whole block, since seed hydrolysis in sep sacch/ferm mode. ; DEFINE CL303C MASS-FLOW STREAM=303C SUBSTREAM=CISOLID & ; COMPONENT=CELLULOS ; DEFINE XM316 STREAM-VAR STREAM=316 SUBSTREAM=MIXED & ; VARIABLE=MASS-FLOW ; DEFINE CI316 STREAM-VAR STREAM=316 SUBSTREAM=CISOLID & ; VARIABLE=MASS-FLOW ; ;C ELOAD IS ENZYME LOADING (FPU / G CELLULOSE) ;F ELOADS = 15.0 ;C ECONC IS ENZYME CONCENTRATION (50 FPU/ML IS APPROX CURRENT IOGEN CONC ;F ECONCS = 50.0 ;C ERAT IS ENZYME RATIO (SOLID ENZYME TO WATER) ;F ERATS = CI316 / (CI316 + XM316) ;C EREQ IS ENZYME REQUIRED (FPU / HR) ;F EREQS = ELOADS * 1000 * (CL303C) ;C DENS IS THE ASSUMED DENSITY OF THE ENZYME (1.000 USED BECAUSE WE ARE ONLY ;C MODELING ENZYME PROTEIN AND WATER; NO CELL MASS OR PRESERVATIVE) (G/ML) ;F DENS = 1.0 ;C EREQM IS THE ENZYME REQUIRED (KG / HR) ;F EREQMS = EREQS / ECONCS * DENS / 1000 ;F CI316 = ERATS * EREQMS ;F XM316 = (1-ERATS) * EREQMS ; READ-VARS CL303C ; WRITE-VARS XM316 CI316 ; ;------------------------------------------------------- ; CELLULASE FORTRAN BLOCKS - AREA 400 ;------------------------------------------------------ ; FORTRAN ENZYME ;F COMMON /CLSSET/ CLYLD, CLPROD, CLVES, CLVOL, CLWV ;THIS BLOCK CALCULTES THE SPLIT IN BLOCK BTMSSPLT SO THAT ;SSCF GETS THE CORRECT ENZYME LOADING. ; ;DEFINE ALL VARIABLES ; CELL1T & CELS1T are sampled only to be printed to verify calculation ; & convergence accuracy ; DEFINE CELL1T MASS-FLOW STREAM=302 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE DEFINE CELS1T MASS-FLOW STREAM=303 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE DEFINE F1 BLOCK-VAR BLOCK=BTMSSPLT SENT=FRAC & VARIABLE=FRAC ID1=401 DEFINE CSDSPT BLOCK-VAR BLOCK=CLFDSPLT SENT=FRAC & VARIABLE=FRAC ID1=403 DEFINE CLIN MASS-FLOW STREAM=232 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE DEFINE XIN MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE CLSSPT BLOCK-VAR BLOCK=CLSSPLIT SENT=FRAC & VARIABLE=FRAC ID1=421 DEFINE CLYLD PARAMETER 41 ; ;FORTRAN STATEMENTS c c MADE CHANGES (*) FOR A SEPARATE SACCHARIFICATION AND FERMENTATION MODE c KI, 3/10/02 c c *Removed SSFSPLT terms from cellulose calc, since in a no SSF mode, c only one stream is going to saccharification and block SSFSPLT c doesn't exist. c c CELL1 is the cellulose flow rate in the primary feed to SSCF. c It could be directly measured, but that causes severe errors for the c first few iterations, so it is being calculated. c F CELL1=CLIN*(1-F1) ;*(1-SSFSPT) c c *No cellulase to seed needed in separate sacch/ferm mode. ;c CELLS1 is the cellulose flow rate in the primary feed to SSCF seed. ;c It could be directly measured, but that causes severe errors for the ;c first few iterations, so it is being calculated. ;c ;F CELLS1=CLIN*(1-F1)*SSFSPT ;c c Enzyme loading ENZYL (FPU/G Cellulose in primary feed) to Saccharification c F ENZYL=0.0000001 c c *No cellulase to seed needed in separate sacch/ferm mode. ;c Enzyme loading ENZYLS (FPU/g Cellulose in primary feed) to SSCF seed ;c ;F ENZYLS=0.0000001 ;c ;c Enzyme Yield ENY FPU/G Cellulose + Xylose (Substrate) is from common block ; (CLYLD) ;c ;F ENY=150. ;c c Cellulase demand by Saccharification c F EZDMD = CELL1 * ENZYL c c *No cellulase to seed needed in separate sacch/ferm mode. c Cellulase demand by SSCF seed c F EZDMDS = 0.0 ;CELLS1 * ENZYLS c c Substrate needed by Cellulase Reactor to Produce Cellulase c F SUBDMD = (EZDMD + EZDMDS) / CLYLD c c Total Substrate is the sum of Cellulase Rxt demand + Seed c F TOTDMD = SUBDMD / (1-CSDSPT) C + ( CSDC + CSDX) c c Split of hydrolyzate to Cellulase Reactors, c CLIN + XIN Total amount of substrate leaving PreHydrolysis c F F1 = TOTDMD / ( CLIN + XIN ) c c *Leave split block in, but 421 will be zero c Split of cellulase broth to SSCF seed and production reactors c F CLSSPT = EZDMDS / (EZDMD + EZDMDS) c F WRITE(NHSTRY,101)CELL1,CELL1T,CELLS1,CELS1T,F1,CSDSPT,CLIN, F 1 XIN,ENZYL F 101 FORMAT(' ENZYME Fortran Block Results',/, F 1 ' FLOWS',/, F 2 ' CELL1 ',g12.5,/, F 3 ' CELL1T ',g12.5,/, F 3 ' CELLS1 ',g12.5,/, F 4 ' CELS1T ',g12.5,/, F 4 ' F1 ',g12.5,/, F 5 ' CSDSPT ',g12.5,/, F 1 ' CLIN ',g12.5,/, F 3 ' XIN ',g12.5,/, F 5 ' ENZYL ',g12.5) F WRITE(NHSTRY,102)ENZYLS,CLYLD,EZDMD,EZDMDS,SUBDMD,TOTDMD,CLSSPT F 102 FORMAT(' ENZYME Fortran Block Results',/, F 1 ' FLOWS',/, F 2 ' ENZYLS ',g12.5,/, F 3 ' ENY ',g12.5,/, F 4 ' EZDMD ',g12.5,/, F 5 ' EZDMDS ',g12.5,/, F 1 ' SUBDMD ',g12.5,/, F 3 ' TOTDMD ',g12.5,/, F 5 ' CLSSPT ',g12.5) ; ; READ-VARS CELL1T CELS1T CSDSPT CLIN XIN CLYLD ; WRITE-VARS F1 CLSSPT EXECUTE BEFORE BTMSSPLT ; FORTRAN NUTRA DEFINE GLUCA MOLE-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE GLUCB MOLE-FLOW STREAM=433 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE ANNOA MOLE-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE ANNOB MOLE-FLOW STREAM=433 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE GALAA MOLE-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE GALAB MOLE-FLOW STREAM=433 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE XYLOA MOLE-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE XYLOB MOLE-FLOW STREAM=433 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE ARABA MOLE-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE ARABB MOLE-FLOW STREAM=433 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE CELLA MOLE-FLOW STREAM=412A SUBSTREAM=CISOLID & COMPONENT=CELLULOS DEFINE CELLB MOLE-FLOW STREAM=433 SUBSTREAM=CISOLID & COMPONENT=CELLULOS DEFINE ANNNA MOLE-FLOW STREAM=412A SUBSTREAM=CISOLID & COMPONENT=MANNAN DEFINE ANNNB MOLE-FLOW STREAM=433 SUBSTREAM=CISOLID & COMPONENT=MANNAN DEFINE GLTNA MOLE-FLOW STREAM=412A SUBSTREAM=CISOLID & COMPONENT=GALACTAN DEFINE GLTNB MOLE-FLOW STREAM=433 SUBSTREAM=CISOLID & COMPONENT=GALACTAN DEFINE ASO2 MOLE-FLOW STREAM=436 SUBSTREAM=MIXED & COMPONENT=SO2 DEFINE ANH3 MOLE-FLOW STREAM=436 SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE xNH3 MOLE-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE yNH3 MOLE-FLOW STREAM=433 SUBSTREAM=MIXED & COMPONENT=NH3 F GLUCOS = GLUCA + GLUCB F ANNOSE = ANNOA + ANNOB F GALAOS = GALAA + GALAB F XYLOSE = XYLOA + XYLOB F ARABOS = ARABA + ARABB F CELLOS = CELLA + CELLB F ANNAN = ANNNA + ANNNB F GLTAN = GLTNA + GLTNB F SO2x = .47*(GLUCOS + ANNOSE + GALAOS + XYLOSE + ARABOS)*0.01522/2. F SO2y = .53*(GLUCOS + ANNOSE + GALAOS + XYLOSE + ARABOS)*0.02414/2. F SO2z = (CELLOS+ANNAN+GLTAN) * 0.02414/2. F ASO2 = SO2x + SO2y + SO2z F ANH3 = ((GLUCOS + ANNOSE + GALAOS + XYLOSE + ARABOS + CELLOS F 1 + ANNAN + GLTAN) * 1./2.) - xNH3 - yNH3 EXECUTE BEFORE F400 ; FORTRAN NUTRB DEFINE GLUC MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE ANNO MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE GALA MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE XYLO MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE ZNH3 MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE ZSO2 MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=SO2 DEFINE ARAB MOLE-FLOW STREAM=431 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE CELL MOLE-FLOW STREAM=431 SUBSTREAM=CISOLID & COMPONENT=CELLULOS DEFINE ANNA MOLE-FLOW STREAM=431 SUBSTREAM=CISOLID & COMPONENT=MANNAN DEFINE GALT MOLE-FLOW STREAM=431 SUBSTREAM=CISOLID & COMPONENT=GALACTAN DEFINE BSO2 MOLE-FLOW STREAM=434 SUBSTREAM=MIXED & COMPONENT=SO2 DEFINE BNH3 MOLE-FLOW STREAM=434 SUBSTREAM=MIXED & COMPONENT=NH3 F BSO2 = (GLUC+ANNO+GALA+XYLO+ARAB+CELL+ANNA+GALT) * 0.01522/2. F 1 - ZSO2 F BNH3 = (GLUC+ANNO+GALA+XYLO+ARAB+CELL+ANNA+GALT) * 1./2. F 1 - ZNH3 FLASH-SPECS 434 TEMP=28.0 PRES=1.0 EXECUTE BEFORE F401-4 ; ;-------------------------------------------------------- ; DISTILLATION FORTRAN BLOCKS - AREA 5000 ;------------------------------------------------------- ; ; Feed forward control for 501 column. Estimates the distillate ; flow and specification bounds for 501 ; FORTRAN FRWD501 IN-UNITS ENG DEFINE D501D BLOCK-VAR BLOCK=D501 VARIABLE=MASS-D & SENTENCE=COL-SPECS DEFINE FEEDC MASS-FLOW STREAM=506 SUBSTREAM=MIXED & COMPONENT=CO2 DEFINE D501DL BLOCK-VAR BLOCK=D501 VARIABLE=LB & SENTENCE=VARY ID1=3 DEFINE D501DH BLOCK-VAR BLOCK=D501 VARIABLE=UB & SENTENCE=VARY ID1=3 DEFINE D501V BLOCK-VAR BLOCK=D501 VARIABLE=MASS-FLOW & SENTENCE=PRODUCTS ID1=510 DEFINE FEEDE MASS-FLOW STREAM=506 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE D501VL BLOCK-VAR BLOCK=D501 VARIABLE=LB & SENTENCE=VARY ID1=2 DEFINE D501VU BLOCK-VAR BLOCK=D501 VARIABLE=UB & SENTENCE=VARY ID1=2 C ASSUME 2/3 OF CO2 GOES OVERHEAD C OVERHEAD SPEC IS 0.8391 MASS FRACTION CO2 F CO2SPC = 0.8391 F WRITE(NTERM, 102) D501D, D501DL, D501DH, D501V, D501VL, D501VU F 102 FORMAT(' D501D ',G12.5,/, F 1 ' D501DL ',G12.5,/, F 2 ' D501DH ',G12.5,/, F 3 ' D501V ',G12.5,/, F 4 ' D501VL ',G12.5,/, F 5 ' D501VU ',G12.5,/) C C SET INITIAL GUESSES FOR DISTILLATIE FLOW C F D501D = (FEEDC ) / CO2SPC C 7936.5 IS A UNITS CONVERSION F D501DL = 0.8 * D501D / 7936.5 F D501DH = 1.2 * D501D / 7936.5 F WRITE(NTERM, 101) D501D, D501DL, D501DH, FEEDC F 101 FORMAT(' D501D ',G12.5,/, F 1 ' D501DL ',G12.5,/, F 2 ' D501DH ',G12.5,/, F 3 ' FEEDC ',G12.5,/) C C SET INITIAL GUESSES FOR VAPOR PRODUCT FLOW C C ASSUME ALL ETHANOL IS IN PRODUCT AND THAT C IT IS 42% BY WEIGHT C F ETHSPC = 0.42 F D501V = FEEDE / ETHSPC F D501VL = D501V * 0.80 / 7936.5 F D501VU = D501V * 1.40 / 7936.5 F WRITE(NTERM,103) D501V, D501VL, D501VU, FEEDE F 103 FORMAT(' D501V ',G12.5,/, F 1 ' D501VL ',G12.5,/, F 2 ' D501VU ',G12.5,/, F 3 ' FEEDE ',G12.5) EXECUTE BEFORE BLOCK D501 ; FORTRAN D502QCR DEFINE FD502 STREAM-VAR STREAM=510 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE Q502R INFO-VAR INFO=HEAT STREAM=QRD502 VARIABLE=DUTY DEFINE Q502C INFO-VAR INFO=HEAT STREAM=QCD502 VARIABLE=DUTY F WRITE(NHSTRY,'('' FORTRAN D502QCR Results'')') F WRITE(NHSTRY,'('' D502 Column Feed = '',g12.5)')fd502 F REBFCT = 6.74933E-5 F CNDFCT = 3.94405E-4 F QR = FD502 * REBFCT F QC = FD502 * CNDFCT F Q502R = QR * (-1E6/3.599948) F Q502C = QC * ( 1E6/3.599948) F WRITE(NHSTRY,'('' D502 Reboiler = '',g12.5,'' MMKcal/hr'')')qr F WRITE(NHSTRY,'('' D502 Reboiler = '',g12.5,'' cal/s'')')q502r F WRITE(NHSTRY,'('' D502 Condenser = '',g12.5,'' MMKcal/hr'')')qc F WRITE(NHSTRY,'('' D502 Condenser = '',g12.5,'' cal/s'')')q502c READ-VARS FD502 WRITE-VARS Q502R Q502C ; ; This FORTRAN Block works with the design-spec CFUGE3S to make ; vary the splits of all of the following components the same ; as water (F1). Water split is being varied by CFUGE3S. CSL Split ; is not controlled by this block. FORTRAN CFUGESLD DEFINE F1 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=1 DEFINE F2 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=2 DEFINE F3 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=3 DEFINE F4 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=4 DEFINE F5 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=5 DEFINE F6 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=6 DEFINE F7 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=7 DEFINE F8 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=8 DEFINE F9 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=9 DEFINE F10 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=10 DEFINE F11 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=11 DEFINE F12 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=12 DEFINE F13 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=13 DEFINE F14 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=14 DEFINE F15 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=15 DEFINE F16 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=16 DEFINE F17 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=17 DEFINE F18 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=18 DEFINE F19 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=19 DEFINE F20 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=20 DEFINE F21 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=21 DEFINE F25 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=25 DEFINE F26 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=26 DEFINE F27 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=27 DEFINE F28 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=28 DEFINE F29 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=29 DEFINE F30 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=30 DEFINE F31 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=31 DEFINE F32 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=32 DEFINE F33 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=33 DEFINE F34 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=34 DEFINE F35 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=35 DEFINE F36 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=36 DEFINE F37 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=37 DEFINE F38 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=38 DEFINE F39 BLOCK-VAR BLOCK=S505 SENTENCE=FRAC & VARIABLE=FRACS ID1=MIXED ID2=571B ELEMENT=39 ; F F2=F1 F F3=F1 F F4=F1 F F5=F1 F F6=F1 F F7=F1 F F8=F1 F F9=F1 F F10=F1 F F11=F1 F F12=F1 F F13=F1 F F14=F1 F F15=F1 F F16=F1 F F17=F1 F F18=F1 F F19=F1 F F20=F1 F F21=F1 F F25=F1 F F26=F1 F F27=F1 F F28=F1 F F29=F1 F F30=F1 F F31=F1 F F32=F1 F F33=F1 F F34=F1 F F35=F1 F F36=F1 F F37=F1 F F38=F1 F F39=F1 ; EXECUTE BEFORE BLOCK S505 ;------------------------------------------------------ ; DIGESTOR FORTRAN BLOCKS - AREA 6000 ;------------------------------------------------------ ; FORTRAN AERAIR F COMMON/ WWLOD2/ COD2, BOD2, CODDY2, BODDY2, BODHP DEFINE AIR STREAM-VAR STREAM=626 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW C THE AIR REQUIREMENT IS 50% ABOVE THEORETICAL (J. RUOCCO) C F XO2 = 2.5*COD2 F AIR=XO2/0.21 EXECUTE BEFORE BLOCK T608 ; FORTRAN RECYCLE ; BLOCK TO CALCULATE THE AMOUNT OF RECYCLE NEEDED AND INCOMING ; FRESH WATER ; ; DEFINE VARIABLES FOR FRESH WATER AND PROCESS RECYCLE WATER DEFINE FWAT STREAM-VAR STREAM=574 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE RWAT STREAM-VAR STREAM=573 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE RWT3 STREAM-VAR STREAM=516 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; ; DEFINE VARIABLES FOR RECYCLE WATER STREAM #2 (Stream. 219). THIS ; STREAM CONTROLS THE SOLIDS CONCENTRATION to fermentation ; DEFINE RV2 STREAM-VAR STREAM=219 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE RI2 STREAM-VAR STREAM=219 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE RGLU MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE RXYE MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE RSSL MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE RARS MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE RGAS MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE RMAS MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE RCSL MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE RCNT MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE RWNT MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE RGLO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE RCLB MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE RXYO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE RMAO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE RGAO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE RARO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE RACO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE RLGS MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE REXT MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE RPRO MASS-FLOW STREAM=219 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; ; DEFINE THE COMPONENTS OF STREAM 232 (Diluted Hydrolysate) ; DEFINE HF1 STREAM-VAR STREAM=232 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE HS1 STREAM-VAR STREAM=232 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE HGLU MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE HXYE MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE HSSL MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE HARS MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE HGAS MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE HMAS MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE HCSL MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE HCNT MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE HWNT MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE HGLO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE HCLB MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE HXYO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE HMAO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE HGAO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE HARO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE HACO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE HLGS MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE HEXT MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE HPRO MASS-FLOW STREAM=232 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; ; DEFINE THE COMPONENTS OF STREAM 401 (Feed to Cellulase Production) ; DEFINE CFF1 STREAM-VAR STREAM=401 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CFS1 STREAM-VAR STREAM=401 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE CFGLU MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE CFXYE MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE CFSSL MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE CFARS MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE CFGAS MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE CFMAS MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE CFCSL MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE CFCNT MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE CFWNT MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE CFGLO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE CFCLB MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE CFXYO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE CFMAO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE CFGAO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE CFARO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE CFACO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE CFLGS MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE CFEXT MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE CFPRO MASS-FLOW STREAM=401 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; ; DEFINE THE COMPONENTS OF STREAM 422 (Cellulase to Ethanol Production) ; DEFINE CPF1 STREAM-VAR STREAM=422 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CPS1 STREAM-VAR STREAM=422 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE CPGLU MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE CPXYE MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE CPSSL MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE CPARS MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE CPGAS MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE CPMAS MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE CPCSL MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE CPCNT MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE CPWNT MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE CPGLO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE CPCLB MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE CPXYO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE CPMAO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE CPGAO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE CPARO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE CPACO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE CPLGS MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE CPEXT MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE CPPRO MASS-FLOW STREAM=422 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; ; DEFINE THE COMPONENTS OF STREAM 311 (DAP to Ethanol Production) ; Changed to DAP by AA 02/21/01 ; Since DAP is only component, do not need to break it out like ; other streams. ; DEFINE DPF1 STREAM-VAR STREAM=311 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE DPS1 STREAM-VAR STREAM=311 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE DPDAP MASS-FLOW STREAM=311 SUBSTREAM=MIXED & COMPONENT=DAP ; ; DEFINE THE COMPONENTS OF STREAM 311A (CSL to Ethanol Production) ; DEFINE CLF1 STREAM-VAR STREAM=311A SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CLS1 STREAM-VAR STREAM=311A SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE CLCSL MASS-FLOW STREAM=311A SUBSTREAM=MIXED & COMPONENT=CSL ; DEFINE THE COMPONENTS OF STREAM 312 (Enzyme to Ethanol Production) ; DEFINE EZF1 STREAM-VAR STREAM=312 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE EZS1 STREAM-VAR STREAM=312 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE EZGLU MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE EZXYE MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE EZSSL MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE EZARS MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE EZGAS MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE EZMAS MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE EZCSL MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE EZCNT MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE EZWNT MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE EZGLO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE EZCLB MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE EZXYO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE EZMAO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE EZGAO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE EZARO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE EZACO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE EZLGS MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE EZEXT MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE EZPRO MASS-FLOW STREAM=312 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; ; DEFINE THE COMPONENTS OF STREAM 303 (Feed to Ferm Seed) ; DEFINE SFF1 STREAM-VAR STREAM=303 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SFS1 STREAM-VAR STREAM=303 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE SFGLU MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE SFXYE MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE SFSSL MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE SFARS MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE SFGAS MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE SFMAS MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE SFCSL MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE SFCNT MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE SFWNT MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE SFGLO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE SFCLB MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE SFXYO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE SFMAO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE SFGAO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE SFARO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE SFACO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE SFLGS MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE SFEXT MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE SFPRO MASS-FLOW STREAM=303 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; ; DEFINE THE COMPONENTS OF STREAM 304 (Seed to Production) ; DEFINE SPF1 STREAM-VAR STREAM=304 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SPS1 STREAM-VAR STREAM=304 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE SPGLU MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE SPXYE MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE SPSSL MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE SPARS MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE SPGAS MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE SPMAS MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE SPCSL MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=CSL DEFINE SPCNT MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=CNUTR DEFINE SPWNT MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=WNUTR DEFINE SPGLO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE SPCLB MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE SPXYO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE SPMAO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE SPGAO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE SPARO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE SPACO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE SPLGS MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE SPEXT MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE SPPRO MASS-FLOW STREAM=304 SUBSTREAM=MIXED & COMPONENT=PROTEIN ; DEFINE VARIABLES FOR RECYCLE WATER STREAM #3. THIS STREAM ; CONTROLS THE XYLOSE AND CELLULOSE CONCENTRATIONS IN 431. ; CURRENTLY, THIS IS SET TO 1%. ; DEFINE CV3 STREAM-VAR STREAM=403 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CI3 STREAM-VAR STREAM=403 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE RI3 STREAM-VAR STREAM=430 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE ST3X MASS-FLOW STREAM=403 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE ST3C MASS-FLOW STREAM=403 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE DEFINE R3X MASS-FLOW STREAM=430 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE R3C MASS-FLOW STREAM=430 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE ; ; DEFINE VARIABLES FOR RECYCLE WATER STREAM #4. THIS STREAM ; CONTROLS THE CELLULOSE CONCENTRATION IN 412A. ; CURRENTLY, THIS IS SET TO 4%. ; DEFINE CV4 STREAM-VAR STREAM=410 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CI4 STREAM-VAR STREAM=410 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE RI4 STREAM-VAR STREAM=411 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE ST4C MASS-FLOW STREAM=410 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE DEFINE R4C MASS-FLOW STREAM=411 SUBSTREAM=CISOLID & COMPONENT=CELLULOSE ; ; DEFINE SPLIT VARIABLES IN THE RECYCLE WATER SPLITTER. ; DEFINE F2 BLOCK-VAR BLOCK=RWSPLT SENT=FRAC & VARIABLE=FRAC ID1=219 DEFINE F3 BLOCK-VAR BLOCK=RWSPLT SENT=FRAC & VARIABLE=FRAC ID1=430 ; ; DEFINE THE COMPONENTS OF STREAM 220 (Out of Pre Hydrolysis ; DEFINE HP1 STREAM-VAR STREAM=220 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE HPS1 STREAM-VAR STREAM=220 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW ; ;FORTRAN STATEMENTS C CSLCONC is the solids concentration of CSL F CSLCONC=0.5 c AV2: Recycle water flow (Stream 219) c CONC2: Total Solids Conc going to Fermentation (Stream 232) c (Includes sugars + solslds) C SLDxxx: Total Solids in Stream C TTLxxx: Total Flow in Stream C CNC219: Total Solids Conc in Stream 219 C OTHSLD: Total Other Solids C OTHTTL: Total Other Flow c c CONC2 is the desired Saccharifiaction effective solids concentration F CONC2 = 0.2 c OLG calcs are the oligomer flows in each stream c SLD calcs are the total solids in each stream F OLG232 = HGLO + HCLB + HXYO + HMAO + HGAO + HARO + HACO F SLD232 = HS1 + HGLU + HXYE + HSSL + HARS + HGAS + HMAS + F 1 (HCSL*CSLCONC) + HCNT + HWNT + HLGS + HEXT + HPRO + F 2 OLG232 F OLG219 = RGLO + RCLB + RXYO + RMAO + RGAO + RARO + RACO F SLD219 = RI2 + RGLU + RXYE + RSSL + RARS + RGAS + RMAS + F 1 (RCSL*CSLCONC) + RCNT + RWNT + RLGS + REXT + RPRO + F 2 OLG219 F OLG401 = CFGLO + CFCLB + CFXYO + CFMAO + CFGAO + CFARO + CFACO F SLD401 = CFS1 + CFGLU + CFXYE + CFSSL + CFARS + CFGAS + CFMAS + F 1 (CFCSL*CSLCONC) + CFCNT + CFWNT + CFLGS + CFEXT + CFPRO + F 2 OLG401 F OLG422 = CPGLO + CPCLB + CPXYO + CPMAO + CPGAO + CPARO + CPACO F SLD422 = CPS1 + CPGLU + CPXYE + CPSSL + CPARS + CPGAS + CPMAS + F 1 (CPCSL*CSLCONC) + CPCNT + CPWNT + CPLGS + CPEXT + CPPRO + F 2 OLG422 c F OLG312 = EZGLO + EZCLB + EZXYO + EZMAO + EZGAO + EZARO + EZACO F SLD312 = EZS1 + EZGLU + EZXYE + EZSSL + EZARS + EZGAS + EZMAS + F 1 (EZCSL*CSLCONC) + EZCNT + EZWNT + EZLGS + EZEXT + EZPRO + F 2 OLG312 c c TTL calc are the total flows of each stream F TTL232 = HF1 + HS1 F TTL219 = RV2 + RI2 F TTL401 = CFF1 + CFS1 F TTL422 = CPF1 + CPS1 F TTL312 = EZF1 + EZS1 F CNC219 = SLD219 / TTL219 F OTHSLD = SLD232 + SLD312 + SLD422 - SLD219 - SLD401 F OTHTTL = TTL232 + TTL312 + TTL422 - TTL219 - TTL401 F CAL219 = ((CONC2 * OTHTTL) - OTHSLD) / (CNC219 - CONC2) c C AV2: Recycle water to hydrolyzate pneumapress F AV2 = CAL219 - RI2 C c c CONC3: Cellulose + Xylose concentration in Stream 431 c AV3: Recycle Flow Stream 430 c F CONC3 = 0.04 F AV3 = ((ST3X + ST3C + R3X + R3C) / CONC3) F 1 - (CI3 + CV3 + RI3) c c CONC4: Cellulose + Xylose in Stream 412A c AV4: Recycle Flow Stream 430 c F CONC4 = 0.04 F AV4 = ((ST4C + R4C) / CONC4) -(CI4 + CV4 + RI4) c c Recalc Concentrations and write to the history file c F CNC2 = (SLD232 - SLD401 + SLD422) / (TTL232 - TTL401 + TTL422) F CNC2b = (RI2 - CFS1 + CPS1 + DPS1 + CLS1 - SFS1 + SPS1) F 1 / (TTL232 - TTL401 + TTL422 ) F CNC3 = (ST3X + ST3C + R3X + R3C) F 1 / (CI3 + CV3 + RI3 + AV3) F CNC4 = (ST4C + R4C) / (CI4 + CV4 + RI4 + AV4) c F WRITE(NHSTRY,101)CNC2,CNC3,CNC4,CNC2b F 101 FORMAT(' RECYCLE Fortran Block Results',/, F 1 ' Specified Concentrations',/, F 3 ' SSCF Effective Solids Conc: ',g12.5,/, F 4 ' Cellulase Seed Feed Cellulose+Xylose (431): ',g12.5,/, F 5 ' Cellulase Ferm Cellulose Conc (412A): ',g12.5,/,/, F 7 ' SSCF Insoluble Solids Conc: ',g12.5) c F WRITE(NHSTRY,151)OTHTTL,OTHSLD,CNC219,CONC2,CAL219 F 151 FORMAT(' RECYCLE Fortran Block Results',/, F 3 ' OTHTTL: ',g12.5,/, F 4 ' OTHSLD: ',g12.5,/, F 5 ' CNC219: ',g12.5,/, F 6 ' CONC2: ',g12.5,/, F 7 ' CAL219: ',g12.5) c c Calculate Splits for Block RWSPLT c F F2=AV2/(AV2+AV3+AV4) F F3=AV3/(AV2+AV3+AV4) F F4=1-F2-F3 c c Calculate Make-up Water, Stream 574 c F RWTAV = RWAT + RWT3 F FWAT= AV2 + RI2 + AV3 + RI3 + AV4 + RI4 - RWTAV EXECUTE BEFORE FWMIX ; FORTRAN RECCOND ; ; DEFINE VARIABLES FOR RECYCLE WATER STREAM #1. THIS STREAM ; CONTROLS THE SOLIDS CONCENTRATION IN THE IMPREGNATOR. ; DEFINE FDV1 STREAM-VAR STREAM=105 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CI1 STREAM-VAR STREAM=214A SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE SSL1 MASS-FLOW STREAM=214A SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE EXT1 MASS-FLOW STREAM=214A SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE PRO1 MASS-FLOW STREAM=214A SUBSTREAM=MIXED & COMPONENT=PROTEIN DEFINE STV1 STREAM-VAR STREAM=215 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE STV2 STREAM-VAR STREAM=216 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE ACV1 STREAM-VAR STREAM=212 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FDV2 STREAM-VAR STREAM=101 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FDS2 STREAM-VAR STREAM=101 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE SSL2 MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE EXT2 MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE PRO2 MASS-FLOW STREAM=101 SUBSTREAM=MIXED & COMPONENT=PROTEIN DEFINE AV1 BLOCK-VAR BLOCK=E501SPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=211 DEFINE DRTSEP BLOCK-VAR BLOCK=C103B SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=104B DEFINE EVPSEP BLOCK-VAR BLOCK=M104LOSS SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=103 DEFINE WAT102 BLOCK-VAR BLOCK=E501SPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=102 c c WSHCNC: Solids concentration after washing (in 105) c 65% from Harris Sub (ACO-9-29067-01) report 99-10600/13 p 4 gives c range of 0.6-0.7 F WSHCNC = 0.65 F CVW = (FDS2 + SSL2 + EXT2 + PRO2) / WSHCNC c c DRT: Fraction of incoming feedstock that is dirt c We do not model/track the dirt; however, water is lost with dirt c separation and disposal c 1% seems reasonable in the near term (D. Templeton & J. Farmer 6 Nov 00) c DRTCNC: Fraction Dirt in dirt disposal stream (remainder is water) c 50% from Harris estimation (J. Lukas email 16 Oct 00) F DRT = 0.01 F DRTCNC = 0.5 F DRTSEP = DRT * (FDV2 + FDS2) * ((1.-DRTCNC)/DRTCNC) c c WATFLO: Total Water flow for washing includes recycle c 5000 gpm (1,140,000 kg/hr) for standard size facility (2000 dry c metric tonne / day @ 15% moisture = 98040 kg/hr) c EVPLOS: Evaporation and Windage Loss as fraction of total water flow c 1% from Harris estimation (J. Lukas email 16 Oct 00) F WATFLO = 1140000 * (FDV2 + FDS2)/98040 F EVPLOS = 0.01 F EVPSEP = EVPLOS * WATFLO c c WAT102: Recycle Water Flow (102) F WAT102 = (CVW - FDV2 - FDS2) + DRTSEP + EVPSEP c c CONC1: Solids Concentration in Reactor, Streams 215A + 216 c F CONC1 = 0.30 F CV1 = ((1.-CONC1)/CONC1) * (CI1 + SSL1 + EXT1 + PRO1) c c AV1 Recycle water flow (Stream 211) c F AV1 = CV1 - STV1 - STV2 - ACV1 - ( FDV1 - SSL1 - EXT1 - PRO1 ) c F CNC1a = CI1 / (CV1 + CI1 + STV1) F CNC1 = CI1 / (CV1 + CI1 + STV1 + STV2) READ-VARS CI1 STV1 STV2 ACV1 FDV2 FDS2 SSL2 FDV1 WRITE-VARS DRTSEP EVPSEP WAT102 AV1 ; EXECUTE BEFORE E501MIX ; FORTRAN CODCALC1 C Calculates the incomming COD F COMMON/ WWLOAD/ CODTOT, BODTOT, CODDAY, BODDAY ; DEFINE CEXTR PARAMETER 13 DEFINE CPRO PARAMETER 14 DEFINE CSOLS PARAMETER 15 ; DEFINE GLUC MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE XYLO MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE UNKN MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=UNKNOWN DEFINE SOLS MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE ARAB MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE GALA MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE XMANS MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE GLUO MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE CELB MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE XYLG MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE XMANO MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE GALO MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE ARAO MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE ACEO MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE XYLL MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=XYLITOL DEFINE ETOH MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE FURF MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=FURFURAL DEFINE XHMF MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=HMF DEFINE CH4 MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=CH4 DEFINE XLACI MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=LACID DEFINE AACI MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=AACID DEFINE GLYC MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=GLYCEROL DEFINE SUCC MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=SUCCACID DEFINE DENA MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=DENAT DEFINE XOIL MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=OIL DEFINE XNNH4 MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=NH4ACET DEFINE SLLGN MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE EXTCT MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE PROTN MASS-FLOW STREAM=613 SUBSTREAM=MIXED & COMPONENT=PROTEIN C C SET THE COD FOR COMPONENTS (KG O2/KG COMPONENT) C THE COD VALUES ARE THE THEORETICAL O2 REQUIRED FOR COMBUSTION, BUT C ONLY FOR SOLUBLE COMPONENTS. INSOLUBLE COMPONENTS ARE ASSUMED TO C BE NON-REACTIVE AND ARE NOT CONTAINED IN THE CALCULATION. C EXTRACTIVE, SOLSOLIDS AND PROTEIN VALUES ARE READ IN BY PARAMETERS C 13, 14, 15. C C SOLUBLE C-CONTAINING COMPOUNDS F CGLUC = 1.07 F CXYLO = 1.07 F CUNKN = 1.07 F CETOH = 2.09 F CARAB = 1.07 F CGALA = 1.07 F CMANS = 1.07 F CGLUO = 1.07 F CCELB = 1.07 F CXYLG = 1.07 F CMANO = 1.07 F CGALO = 1.07 F CARAO = 1.07 F CXYLL = 1.22 F CFURF = 1.67 F CHMF = 1.52 F CCH4 = 4.0 F CLACI = 1.07 F CAACI = 1.07 F CGLYC = 1.22 F CSUCC = 0.95 F CDENA = 3.52 F COIL = 2.89 F CACEO = 1.07 F CNNH4 = 1.143 F CSLGN = 1.6000 C C C CALCULATE HOURLY COD LOADINGS (KG/HR) C F CODTOT = GLUC*CGLUC + XYLO*CXYLO + UNKN*CUNKN + SOLS*CSOLS + F 1 GALA*CGALA + XMANS*CMANS + ARAB*CARAB + GLUO*CGLUO + F 2 CELB*CCELB + XYLG*CXYLG + XMANO*CMANO + GALO*CGALO + F 3 ARAO*CARAO + XYLL*CXYLL + ETOH*CETOH + FURF*CFURF + F 4 XHMF*CHMF + CH4*CCH4 + XLACI*CLACI + AACI*CAACI + F 5 GLYC*CGLYC + SUCC*CSUCC + DENA*CDENA + XOIL*COIL + F 6 ACEO*CACEO + CNNH4*XNNH4 + SLLGN*CSLGN + EXTCT*CEXTR + F 7 PROTN*CPRO C C C CALCULATE HOURLY BOD LOADINGS (KG/HR) C F BODCOD = 0.70 C BODCOD IS THE BOD/COD RATIO AND WAS PROVIDED BY J. RUOCCO 7/29/98 C THIS VALUE IS WITHIN THE RANGE (0.45-0.78) PROVIDED IN PERRY'S C 7TH EDITION, PG. 25-62. C F BODTOT= BODCOD*CODTOT C C C CALCULATE DAILY BOD AND COD LOADINGS (LB/DAY) C F CODDAY = CODTOT*2.205*24. F BODDAY = BODTOT*2.205*24. C C 2.205 IS LB/KG AND 24 HR/DAY TO CONVERT KG/HR TO LB/DAY C C WRITE ANSWERS TO THE HISTORY FILE C F WRITE(NHSTRY,*)'CODTOT, BODTOT= ',CODTOT, BODTOT F WRITE(NHSTRY,*)'CODDAY, BODDAY= ',CODDAY, BODDAY C C New 11/23/98 DEFINE TOTANA STREAM-PROP STREAM=632 PROPERTY=MASSFLW C C Anerobic Space velocity Rucco, G/L/D C F ANLOAD = 12.0 F ANCONC = (CODTOT*1000.)/TOTANA F ANRT = (ANCONC*24.0)/ANLOAD C Calculate Anerobic volume in gallons F ANVOL1 = (TOTANA*ANRT)/3.7854 DEFINE ANROHP INFO-VAR STREAM=WT606 INFO=WORK VARIABLE=POWER C Assume HP 0.05 hp / 1000 gal F ANRHP = 0.05 * ANVOL1 / 1000. C Convert to KW F ANROHP = ANRHP * 0.7457 F WRITE(NHSTRY,*)'ANVOL1=',ANVOL1,' ANRHP=',ANRHP C READ-VARS GLUC TOTANA CEXTR CPRO CSOLS WRITE-VARS ANROHP FORTRAN CODCALC2 C Calculates COD after ANEROBIC and before AEROBIC F COMMON/ WWLOD2/ COD2, BOD2, CODDY2, BODDY2, BODHP DEFINE CEXTR PARAMETER 13 DEFINE CPRO PARAMETER 14 DEFINE CSOLS PARAMETER 15 DEFINE GLUC MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE XYLO MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE UNKN MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=UNKNOWN DEFINE SOLS MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE ARAB MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE GALA MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE XMANS MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE GLUO MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE CELB MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE XYLG MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE XMANO MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE GALO MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE ARAO MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE ACEO MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE XYLL MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=XYLITOL DEFINE ETOH MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE FURF MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=FURFURAL DEFINE XHMF MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=HMF DEFINE CH4 MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=CH4 DEFINE XLACI MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=LACID DEFINE AACI MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=AACID DEFINE GLYC MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=GLYCEROL DEFINE SUCC MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=SUCCACID DEFINE DENA MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=DENAT DEFINE XOIL MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=OIL DEFINE XNNH4 MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=NH4ACET DEFINE SLLGN MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE EXTCT MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE PROTN MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=PROTEIN C C SET THE COD FOR COMPONENTS (KG O2/KG COMPONENT) C THE COD VALUES ARE THE THEORETICAL O2 REQUIRED FOR COMBUSTION, BUT C ONLY FOR SOLUBLE COMPONENTS. INSOLUBLE COMPONENTS ARE ASSUMED TO C BE NON-REACTIVE AND ARE NOT CONTAINED IN THE CALCULATION. C EXTRACTIVE, SOLSOLIDS AND PROTEIN VALUES ARE READ IN BY PARAMETERS C 13, 14, 15. C C SOLUBLE C-CONTAINING COMPOUNDS F CGLUC = 1.07 F CXYLO = 1.07 F CUNKN = 1.07 F CETOH = 2.09 F CARAB = 1.07 F CGALA = 1.07 F CMANS = 1.07 F CGLUO = 1.07 F CCELB = 1.07 F CXYLG = 1.07 F CMANO = 1.07 F CGALO = 1.07 F CARAO = 1.07 F CXYLL = 1.22 F CFURF = 1.67 F CHMF = 1.52 F CCH4 = 4.0 F CLACI = 1.07 F CAACI = 1.07 F CGLYC = 1.22 F CSUCC = 0.95 F CDENA = 3.52 F COIL = 2.89 F CACEO = 1.07 F CNNH4 = 1.143 F CSLGN = 1.6000 C C CALCULATE HOURLY COD LOADINGS (KG/HR) C F COD2 = GLUC*CGLUC + XYLO*CXYLO + UNKN*CUNKN + SOLS*CSOLS + F 1 GALA*CGALA + XMANS*CMANS + ARAB*CARAB + GLUO*CGLUO + F 2 CELB*CCELB + XYLG*CXYLG + XMANO*CMANO + GALO*CGALO + F 3 ARAO*CARAO + XYLL*CXYLL + ETOH*CETOH + FURF*CFURF + F 4 XHMF*CHMF + CH4*CCH4 + XLACI*CLACI + AACI*CAACI + F 5 GLYC*CGLYC + SUCC*CSUCC + DENA*CDENA + XOIL*COIL + F 6 ACEO*CACEO + CNNH4*XNNH4 + SLLGN*CSLGN + EXTCT*CEXTR + F 7 PROTN*CPRO C C C CALCULATE HOURLY BOD LOADINGS (KG/HR) C F BODCOD = 0.70 C BODCOD IS THE BOD/COD RATIO AND WAS PROVIDED BY J. RUOCCO 7/29/98 C THIS VALUE IS WITHIN THE RANGE (0.45-0.78) PROVIDED IN PERRY'S C 7TH EDITION, PG. 25-62. C F BOD2 = BODCOD*COD2 C C C CALCULATE DAILY BOD AND COD LOADINGS (LB/DAY) C F CODDY2 = COD2*2.205*24. F BODDY2 = BOD2*2.205*24. C C 2.205 IS LB/KG AND 24 HR/DAY TO CONVERT KG/HR TO LB/DAY C C WRITE ANSWERS TO THE HISTORY FILE C F WRITE(NHSTRY,*)'COD2, BOD2= ',COD2, BOD2 F WRITE(NHSTRY,*)'CODDY2, BODDY2= ',CODDY2, BODDY2 C ** New 11/23/98 C Per the Mereick quote from Goble Sampson, calculate the hp C necessary for Aerobic Aeration C C Calculate the O2, lb per day, 2 lb O2 per lb BOD C F BOD2O2 = BODDY2 * 2. C C Calculate Hp per Goble Sampson Quote C F BODHP = BOD2O2 / (0.616 * 64.8) C DEFINE AEROHP INFO-VAR STREAM=WT608 INFO=WORK VARIABLE=POWER F AEROHP = BODHP * 0.7457 F WRITE(NHSTRY,*)'AEROHP=',AEROHP,' BODHP=',BODHP READ-VARS GLUC CEXTR CPRO CSOLS WRITE-VARS AEROHP FORTRAN CODEND C Calculates the final COD level in the waste water F COMMON/ WWLOD3/ COD3, BOD3, CODDY3, BODDY3 DEFINE CEXTR PARAMETER 13 DEFINE CPRO PARAMETER 14 DEFINE CSOLS PARAMETER 15 DEFINE GLUC MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=GLUCOSE DEFINE XYLO MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE UNKN MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=UNKNOWN DEFINE SOLS MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=SOLSLDS DEFINE ARAB MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=ARABINOS DEFINE GALA MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=GALACTOS DEFINE XMANS MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=MANNOSE DEFINE GLUO MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=GLUCOLIG DEFINE CELB MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=CELLOB DEFINE XYLG MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=XYLOLIG DEFINE XMANO MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=MANOLIG DEFINE GALO MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=GALAOLIG DEFINE ARAO MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=ARABOLIG DEFINE ACEO MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=ACETOLIG DEFINE XYLL MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=XYLITOL DEFINE ETOH MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=ETHANOL DEFINE FURF MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=FURFURAL DEFINE XHMF MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=HMF DEFINE CH4 MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=CH4 DEFINE XLACI MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=LACID DEFINE AACI MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=AACID DEFINE GLYC MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=GLYCEROL DEFINE SUCC MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=SUCCACID DEFINE DENA MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=DENAT DEFINE XOIL MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=OIL DEFINE XNNH4 MASS-FLOW STREAM=624 SUBSTREAM=MIXED & COMPONENT=NH4ACET DEFINE SLLGN MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=LGNSOL DEFINE EXTCT MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=EXTRACT DEFINE PROTN MASS-FLOW STREAM=618 SUBSTREAM=MIXED & COMPONENT=PROTEIN C C SET THE COD FOR COMPONENTS (KG O2/KG COMPONENT) C THE COD VALUES ARE THE THEORETICAL O2 REQUIRED FOR COMBUSTION, BUT C ONLY FOR SOLUBLE COMPONENTS. INSOLUBLE COMPONENTS ARE ASSUMED TO C BE NON-REACTIVE AND ARE NOT CONTAINED IN THE CALCULATION. C EXTRACTIVE, SOLSOLIDS AND PROTEIN VALUES ARE READ IN BY PARAMETERS C 13, 14, 15. C C SOLUBLE C-CONTAINING COMPOUNDS F CGLUC = 1.07 F CXYLO = 1.07 F CUNKN = 1.07 F CETOH = 2.09 F CARAB = 1.07 F CGALA = 1.07 F CMANS = 1.07 F CGLUO = 1.07 F CCELB = 1.07 F CXYLG = 1.07 F CMANO = 1.07 F CGALO = 1.07 F CARAO = 1.07 F CXYLL = 1.22 F CFURF = 1.67 F CHMF = 1.52 F CCH4 = 4.0 F CLACI = 1.07 F CAACI = 1.07 F CGLYC = 1.22 F CSUCC = 0.95 F CDENA = 3.52 F COIL = 2.89 F CACEO = 1.07 F CNNH4 = 1.143 F CSLGN = 1.6000 C C C CALCULATE HOURLY COD LOADINGS (KG/HR) C F COD3 = GLUC*CGLUC + XYLO*CXYLO + UNKN*CUNKN + SOLS*CSOLS + F 1 GALA*CGALA + XMANS*CMANS + ARAB*CARAB + GLUO*CGLUO + F 2 CELB*CCELB + XYLG*CXYLG + XMANO*CMANO + GALO*CGALO + F 3 ARAO*CARAO + XYLL*CXYLL + ETOH*CETOH + FURF*CFURF + F 4 XHMF*CHMF + CH4*CCH4 + XLACI*CLACI + AACI*CAACI + F 5 GLYC*CGLYC + SUCC*CSUCC + DENA*CDENA + XOIL*COIL + F 6 ACEO*CACEO + CNNH4*XNNH4 + SLLGN*CSLGN + EXTCT*CEXTR + F 7 PROTN*CPRO C C C CALCULATE HOURLY BOD LOADINGS (KG/HR) C F BODCOD = 0.70 C BODCOD IS THE BOD/COD RATIO AND WAS PROVIDED BY J. RUOCCO 7/29/98 C THIS VALUE IS WITHIN THE RANGE (0.45-0.78) PROVIDED IN PERRY'S C 7TH EDITION, PG. 25-62. C F BOD3 = BODCOD*COD3 C C C CALCULATE DAILY BOD AND COD LOADINGS (LB/DAY) C F CODDY3 = COD3*2.205*24. F BODDY3 = BOD3*2.205*24. C C 2.205 IS LB/KG AND 24 HR/DAY TO CONVERT KG/HR TO LB/DAY C C WRITE ANSWERS TO THE HISTORY FILE C F WRITE(NHSTRY,*)'COD3, BOD3= ',COD3, BOD3 F WRITE(NHSTRY,*)'CODDY3, BODDY3= ',CODDY3, BODDY3 C READ-VARS GLUC CEXTR CPRO CSOLS ; FORTRAN WWNUTR1 F COMMON/ WWLOAD/ CODTOT, BODTOT, CODDAY, BODDAY DEFINE WWTNUT STREAM-VAR STREAM=630 SUBSTREAM=MIXED VARIABLE=MASS-FLOW C F WWTFAC = 3.675E-2 C C THE AMOUNT OF PHOSPHORIC ACID, UREA, MICRONUTRIENTS AND CAUSTIC C F WWTNUT = WWTFAC*CODTOT C EXECUTE AFTER FORTRAN CODCALC1 FORTRAN WWNUTR2 F COMMON/ WWLOD2/ COD2, BOD2, CODDY2, BODDY2, BODHP DEFINE WWTNUT STREAM-VAR STREAM=631 SUBSTREAM=MIXED VARIABLE=MASS-FLOW C F WWTFAC = 1.701E-3 C C WWTFAC IS THE AMOUNT OF POLYMER ADDED LB/LB COD TO THE AEROBIC C SYSTEM. IT IS THE AVERAGE VALUE PROVIDED BY J. RUOCCO FOR THE C 3 SYSTEM DESIGNS (ENZYME, COUNTERCURRENT AND SOFTWOOD) C POLYMER IS MODELLED AS THE COMPONENT WNUTR C F WWTNUT = WWTFAC*COD2 C EXECUTE AFTER FORTRAN CODCALC2 ;------------------------------------------------------- ; STORAGE FORTRAN BLOCKS - AREA 7000 ;------------------------------------------------------ ; FORTRAN CSL-ENZY ; This FORTRAN block calculates the CSL requirements of ; the Cellulase Production and Seed Fermentation ; Streams 414 and 423 ; Also calculates the "Other Nutrients" demand, Stream 415 ; Finally the total CLS requirements are calculated and ; the flow of 735 set ; ; INPUT FLOWS DEFINE CF STREAM-VAR STREAM=412A SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CFS STREAM-VAR STREAM=433 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CND STREAM-VAR STREAM=436 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SD STREAM-VAR STREAM=431 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SND STREAM-VAR STREAM=434 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FSCLS MASS-FLOW STREAM=310A SUBSTREAM=MIXED & COMPONENT=CSL DEFINE FCLS MASS-FLOW STREAM=311A SUBSTREAM=MIXED & COMPONENT=CSL ; INPUT DENSITIES DEFINE CFD STREAM-VAR STREAM=412A SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE CFSD STREAM-VAR STREAM=433 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE CODD STREAM-VAR STREAM=417 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE CNDD STREAM-VAR STREAM=436 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY ; OUTPUTS DEFINE CLSP STREAM-VAR STREAM=414 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CLSS STREAM-VAR STREAM=423 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CLNUTR STREAM-VAR STREAM=415 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE TTLCSL STREAM-VAR STREAM=735 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CO STREAM-VAR STREAM=417 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW c F CLD = 0.01 c CLD IS THE DEMAND FOR CSL IN CELLULASE PRODUCTION IN KG/KG F CLSP = CLD * (CF + CFS + CND) c F CLSD = 0.01 c CLSD IS THE DEMAND FOR CSL IN CELLULASE SEED PRODUCTION IN KG/KG F CLSS = CLSD * (SD + SND) c c CN IS THE CELLULASE NUTRIENT DEMAND IN LB/LB TOTAL STREAM c THIS VALUE IS FROM THE BASE CASE & SHOULD BE UPDATED WITH c NEW DATA. 0.0043 = 4.3 g/L from the 1991 base case (1.4 g/L c ammonium sulfate, 2.0 g/L potassium phosphate, 0.3 g/L magnesium c sulfate*7H2O, 0.4 g/L calcium chloride*2H2O, & 0.2 g/L Tween 80. c F CN = 0.0043 F CLNUTR = CN * (CF + CFS + CND) c Calculate the total CSL used F TTLCSL = CLSS + CLSP + FSCLS + FCLS C F COD=0.001 c COD IS THE CORN OIL DEMAND IN L/L (AntiFoam) c F CO = COD * (CF/CFD + CFS/CFSD + CND/CNDD) * CODD C READ-VARS CF CFS CND SD SND FSCLS FCLS CFD CFSD & CODD CNDD WRITE-VARS CLSP CLSS CLNUTR TTLCSL CO FORTRAN DENATURE ;THIS BLOCK CALCULATES THE AMOUNT OF DENATURANT REQUIRED. ;IT ALSO CALCULATES THE SIZE OF THE GASOLINE (DENATURANT) ;TANK. ; INPUTS DEFINE PDENS STREAM-VAR STREAM=515E SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE PROD STREAM-VAR STREAM=515E SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE GDENS STREAM-VAR STREAM=701 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY ; OUTPUT DEFINE GGAS STREAM-VAR STREAM=701 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; ;SPECIFY THE DENATURANT ADDITION (PART DENAT / 100 PARTS ETHANOL FUEL) ;4.75 PER MARK RUTH MEMO 3 NOVEMBER 1999 ; F DPERC = 4.75 c c CALCULATE THE FLOWRATE OF DENATURANT INTO THE SYSTEM. c F GGAS = DPERC / 100 * (PROD / PDENS) * GDENS c READ-VARS PDENS PROD GDENS WRITE-VARS GGAS ; EXECUTE AFTER T507-8 ; FORTRAN STORE ; ; Sums up various Tank Farm Flows and Sets others, like ; Diesel, & Fire Water as ratios of Ethanol Product ; ; INPUTS DEFINE PRFLOW STREAM-VAR STREAM=515 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE AFLOW1 STREAM-VAR STREAM=212 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE AFLOW2 STREAM-VAR STREAM=233 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE AMFLW2 MASS-FLOW STREAM=434 SUBSTREAM=MIXED & COMPONENT=NH3 DEFINE AMFLW3 MASS-FLOW STREAM=436 SUBSTREAM=MIXED & COMPONENT=NH3 ; ; DAP is SSCF nutrient, Phosphorus source likely. DEFINE APFLW1 MASS-FLOW STREAM=310 SUBSTREAM=MIXED & COMPONENT=DAP DEFINE APFLW2 MASS-FLOW STREAM=311 SUBSTREAM=MIXED & COMPONENT=DAP DEFINE ALFLW2 STREAM-VAR STREAM=227 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW ; Enzyme required DEFINE F312M STREAM-VAR STREAM=312 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE F312S STREAM-VAR STREAM=312 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW ; OUTPUTS DEFINE TAFLOW STREAM-VAR STREAM=710 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FWFLOW STREAM-VAR STREAM=713 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE TAMFLW STREAM-VAR STREAM=717 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE DFLOW STREAM-VAR STREAM=723 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE TLFLOW STREAM-VAR STREAM=745 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE F750M STREAM-VAR STREAM=750 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE F750S STREAM-VAR STREAM=750 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE TAPFLW STREAM-VAR STREAM=755 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; Acid Flows F TAFLOW = AFLOW1 + AFLOW2 ; ; Lime Flows F TLFLOW = ALFLW2 ; c CALCULATE THE FIREWATER TANK (T704) VARIABLES c c THE FIREWATER FLOWRATE IS SCALED FROM THE ORIGINAL BASE CASE c ETHANOL PRODUCT FLOWRATE (PROD) c F PROD = 21769. F FWFLOW = 8007 * PRFLOW / PROD c c CALCULATE THE AMMONIA STORAGE SYSTEM c c DNH3 is the ammonia req per ethanol produced (lb/lb) F TAMFLW = AMFLW2 + AMFLW3 c c CALCULATE THE DIESEL FUEL TANK. IT WILL BE SIMILAR TO THAT FOR c THE FIREWATER TANK AND WILL BE SCALED OFF OF THE PRODUCT FLOWRATE. c F BCDF = 519.7 c BCDF IS THE BASE CASE DIESEL FLOWRATE IN KG/HR c C BCPF IS THE BASE CASE PROPANE FLOWRATE IN KG/HR C A 33 LB PROPANE TANK WILL LAST 8 HOURS ACCORDING TO QUOTE FROM C HARRIS GROUP C Therefore, 33 lb / 8 hr = 4.125 lb/hr for a single forklift C 8 fork lifts required for base case C 4.125 lb/hr * 8 = 33 lb/hr / 2.205 = 14.97 kg/hr c F BCPF = 14.97 F PROD2 = 18285. C PROD2 set at 18285 for model A0102Q. F DFLOW = BCPF * PRFLOW / PROD2 c c Calculate Cellase flow to whole facility F F750M = F312M ; + F316M F F750S = F312S ; + F316S C C Calculate DAP flow to whole facility F TAPFLW = APFLW1 + APFLW2 C EXECUTE AFTER T507-8 ; FORTRAN CHEMICAL ; ;CALCULATE BFW & COOLING TOWER CHEMICALS. ;VALUES ARE SCALED FROM THE SPREADSHEET VALUES. ; DEFINE BFLOW STREAM-VAR STREAM=811 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FLXTRA STREAM-VAR STREAM=251 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE BFC STREAM-VAR STREAM=921 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CWF STREAM-VAR STREAM=947 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CWC STREAM-VAR STREAM=922 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ;ASSUME BFW CHEMICALS ARE NEEDED FOR THE WATER FED TO IX ;DEFINE RATIOS OF CHEMICALS ; F BFCREQ=7.E-6 c BFCREQ IS THE BFW CHEMICAL REQ IN LB/LB BFW ; Requirement from Radian Report. Back-calculated from cases. c F CWCREQ=2.E-7 c CWCREQ IS THE COOLING TOWER CHEMICAL REQ c IN LB/LB COOLING WATER FLOW c c Check to see if there is more clean recycle water than 811 makeup: F IF (BFLOW.GT.FLXTRA) THEN F BFC=BFCREQ*(BFLOW - FLXTRA) F ELSE F BFC=1.0 F END IF F CWC=CWCREQ*CWF c READ-VARS BFLOW CWF FLXTRA WRITE-VARS BFC CWC ; EXECUTE AFTER T914 ;------------------------------------------------------------- ; BURNER FORTRAN BLOCKS - AREA 800 ;------------------------------------------------------------ ; FORTRAN O2CALC DEFINE CH4615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE X2S615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=H2S DEFINE FUR615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=HMF DEFINE AA615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=AACID DEFINE CH4840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE SOL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE CEL840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE ARN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE XLG840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE ACE840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE EXS840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=UNKNOWN DEFINE GLO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XNO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XYO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE TAR840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE FUR840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=HMF DEFINE XLL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE GLU840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE XNS840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GAL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE ARA840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE AA840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=AACID DEFINE XLA840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=LACID DEFINE CLS840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CELLULAS DEFINE ETO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE ZYM840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE GLY840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE BIO840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE C840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=C DEFINE UNK840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=H2S DEFINE ACN840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE COI840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=OIL DEFINE DEN840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE XSL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=PROTEIN DEFINE SOL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE CEL803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE ARN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE XLG803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE ACE803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE EXS803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=UNKNOWN DEFINE GLO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XNO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XYO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE TAR803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE FUR803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=HMF DEFINE XLL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE GLU803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE XNS803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GAL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE ARA803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE AA803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=AACID DEFINE XLA803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=LACID DEFINE CLS803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=CELLULAS DEFINE ETO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE ZYM803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE GLY803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE BIO803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE C803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=C DEFINE UNK803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=H2S DEFINE ACN803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE COI803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=OIL DEFINE DEN803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE XSL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=PROTEIN DEFINE FRACO2 MASS-FRAC STREAM=804 SUBSTREAM=MIXED COMPONENT=O2 DEFINE BNDLOW PARAMETER 55 DEFINE BNDHIH PARAMETER 56 C SET THE MOLES OF OXYGEN REQUIRED TO COMBUST 1 MOLE OF EACH COMPONENT C THE VARIABLES ARE ROXXX WITH THE 3 X'S CORRESPONDING C TO A 3 LETTER CODE FOR EACH COMPONENT USED IN THE DEFINE STATEMENTS C F ROCH4 = 2.0 F ROX2S = 1.5 F ROFUR = 5.0 F ROXMF = 6.0 F ROAA = 2.0 F ROSOL = 0.4352 F ROCEL = 6.0 F ROXYN = 5.0 F ROARN = 5.0 F ROXNN = 6.0 F ROGAN = 6.0 F ROXLG = 12.825 F ROACE = 2.0 F ROGLO = 6.0 F ROCLB = 12.0 F ROXNO = 6.0 F ROGAO = 6.0 F ROARO = 5.0 F ROXYO = 5.0 F ROTAR = 5.0 F ROACO = 2.0 F ROXLL = 5.5 F ROGLU = 6.0 F ROXYL = 5.0 F ROXNS = 6.0 F ROGAL = 6.0 F ROARA = 5.0 F ROXLA = 3.0 F ROCLS = 1.2445 F ROETO = 3.0 F ROZYM = 1.2 F ROGLY = 3.5 F ROSUC = 3.5 F ROBIO = 1.2185 F ROACN = 2.75 F ROCOI = 25.5 F ROXLGS = 12.825 F ROEXT = 0.4352 F ROPRO = 0.4352 F ROC = 1.0 F RODEN = 11.0 c UNKNOWN component is currently not being used so ROEXS=0.0 c & ROUNK=0.0 MR 14 Nov 00 F ROEXS = 0.0 F ROUNK = 0.0 C C CALCULATE THE O2 REQUIREMENT TO COMBUST STREAM 615, ANAEROBIC OFF-GAS C F RO615 = CH4615*ROCH4 + X2S615*ROX2S + FUR615*ROFUR + F 1 XMF615*RO615 + AA615*RO615 F WRITE(NHSTRY,*)'REQUIRED OXYGEN FOR 615 (MOLE/HR)= ',RO615 C C CALCULATE THE O2 REQUIREMENT TO COMBUST OF STREAM 840, SUPPLEMENT to boiler C F RO840 = CH4840*ROCH4 + F 1 SOL840*ROSOL + CEL840*ROCEL + XYN840*ROXYN + F 2 ARN840*ROARN + XNN840*ROXNN + GAN840*ROGAN + F 3 XLG840*ROXLG + ACE840*ROACE + EXS840*ROEXS + F 4 GLO840*ROGLO + CLB840*ROCLB + XNO840*ROXNO + F 5 GAO840*ROGAO + ARO840*ROARO + XYO840*ROXYO + F 6 TAR840*ROTAR + ACO840*ROACO + FUR840*ROFUR + F 7 XMF840*ROXMF + XLL840*ROXLL + GLU840*ROGLU + F 8 XYL840*ROXYL + XNS840*ROXNS + GAL840*ROGAL + F 9 ARA840*ROARA + AA840*ROAA + XLA840*ROXLA + F * CLS840*ROCLS + ETO840*ROETO + ZYM840*ROZYM + F 1 GLY840*ROGLY + SUC840*ROSUC + BIO840*ROBIO + F 2 C840*ROC + UNK840*ROUNK + X2S840*ROX2S + F 3 ACN840*ROACN + COI840*ROCOI + DEN840*RODEN + F 4 XSL840*ROXLGS + EXT840*ROEXT + PRO840*ROPRO F WRITE(NHSTRY,*)'REQUIRED OXYGEN FOR 840 (MOLE/HR)= ',RO840 C C CALCULATE THE BTU/HR OF STREAM 803:S505 SOLIDS,DIGESTOR SOLIDS,SYRUP C F RO803 = SOL803*ROSOL + CEL803*ROCEL + XYN803*ROXYN + F 1 ARN803*ROARN + XNN803*ROXNN + GAN803*ROGAN + F 2 XLG803*ROXLG + ACE803*ROACE + EXS803*ROEXS + F 3 GLO803*ROGLO + CLB803*ROCLB + XNO803*ROXNO + F 4 GAO803*ROGAO + ARO803*ROARO + XYO803*ROXYO + F 5 TAR803*ROTAR + ACO803*ROACO + FUR803*ROFUR + F 6 XMF803*ROXMF + XLL803*ROXLL + GLU803*ROGLU + F 7 XYL803*ROXYL + XNS803*ROXNS + GAL803*ROGAL + F 8 ARA803*ROARA + AA803*ROAA + XLA803*ROXLA + F 9 CLS803*ROCLS + ETO803*ROETO + ZYM803*ROZYM + F * GLY803*ROGLY + SUC803*ROSUC + BIO803*ROBIO + F 1 C803*ROC + UNK803*ROUNK + X2S803*ROX2S + F 2 ACN803*ROACN + COI803*ROCOI + DEN803*RODEN + F 3 XSL803*ROXLGS + EXT803*ROEXT + PRO803*ROPRO F WRITE(NHSTRY,*)'REQUIRED OXYGEN FOR 803 (MOLE/HR)= ',RO803 C C CALCULATE THE TOTAL OXYGEN REQUIREMENT OF THE BOILER (MOLE/HR) C F ROTMOL = (RO615+RO840+RO803) C C CALCULATE THE TOTAL OXYGEN REQUIREMENT OF THE BOILER + EXCESS (KG/HR) F ROTMAS = ROTMOL * 32 * 1.2 C C WRITE RESULTS TO THE HISTORY FILE C F WRITE(NHSTRY,*)'REQUIRED OXYGEN MOLE FLOW (NO EXCESS)= ',ROTMOL F WRITE(NHSTRY,*)'REQUIRED OXYGEN MASS FLOW= ',ROTMAS C C SET UPPER AND LOWER BOUNDS FOR COMBAIR C F BNDLOW = ROTMAS * 0.8 / FRACO2 F BNDHIH = ROTMAS * 1.2 / FRACO2 C READ-VARS AA615 CH4840 XLG803 FRACO2 WRITE-VARS BNDLOW BNDHIH ; FORTRAN COMBHEAT F COMMON / HEATIN / BTUTOT ; ; Needed for the HHV of the inlet biomass feed. DEFINE BTU101 PARAMETER 4 DEFINE CH4101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE SOL101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE CEL101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE ARN101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE XLG101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE ACE101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE EXS101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=UNKNOWN DEFINE GLO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XNO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XYO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE TAR101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE FUR101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=HMF DEFINE XLL101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE GLU101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE XNS101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GAL101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE ARA101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE AA101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=AACID DEFINE XLA101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=LACID DEFINE CLS101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=CELLULAS DEFINE ETO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE ZYM101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE GLY101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE BIO101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE C101 MASS-FLOW STREAM=101 SUBSTREAM=CISOLID COMPONENT=C DEFINE UNK101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=H2S DEFINE ACN101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE COI101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=OIL DEFINE DEN101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE XSL101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO101 MASS-FLOW STREAM=101 SUBSTREAM=MIXED COMPONENT=PROTEIN ; DEFINE CH4615 MASS-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE X2S615 MASS-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=H2S DEFINE FUR615 MASS-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF615 MASS-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=HMF DEFINE AA615 MASS-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=AACID DEFINE CH4840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE SOL840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE CEL840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE ARN840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE XLG840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE ACE840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE EXS840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=UNKNOWN DEFINE GLO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XNO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XYO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE TAR840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE FUR840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=HMF DEFINE XLL840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE GLU840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE XNS840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GAL840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE ARA840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE AA840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=AACID DEFINE XLA840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=LACID DEFINE CLS840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CELLULAS DEFINE ETO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE ZYM840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE GLY840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE BIO840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE C840 MASS-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=C DEFINE UNK840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=H2S DEFINE ACN840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE COI840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=OIL DEFINE DEN840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE XSL840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=PROTEIN DEFINE SOL803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE CEL803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE ARN803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE XLG803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE ACE803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE EXS803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=UNKNOWN DEFINE GLO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XNO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XYO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE TAR803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE FUR803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=HMF DEFINE XLL803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE GLU803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE XNS803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GAL803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE ARA803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE AA803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=AACID DEFINE XLA803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=LACID DEFINE CLS803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=CELLULAS DEFINE ETO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE ZYM803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE GLY803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE BIO803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE C803 MASS-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=C DEFINE UNK803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=H2S DEFINE ACN803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE COI803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=OIL DEFINE DEN803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE XSL803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=PROTEIN DEFINE SOL531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE CEL531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE ARN531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE XLG531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE ACE531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE EXS531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=UNKNOWN DEFINE GLO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XNO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XYO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE TAR531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE FUR531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=HMF DEFINE XLL531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE GLU531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE XNS531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GAL531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE ARA531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE AA531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=AACID DEFINE XLA531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=LACID DEFINE CLS531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=CELLULAS DEFINE ETO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE ZYM531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE GLY531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE BIO531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE C531 MASS-FLOW STREAM=531 SUBSTREAM=CISOLID COMPONENT=C DEFINE UNK531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=H2S DEFINE ACN531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE COI531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=OIL DEFINE DEN531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE XSL531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO531 MASS-FLOW STREAM=531 SUBSTREAM=MIXED COMPONENT=PROTEIN C SET THE HEAT OF COMBUSTION (HHVs) FOR EACH COMPONENT C THE HEAT OF COMBUSTIONS ARE IN BTU/KG C THE VARIABLES ARE HCXXX WITH THE 3 X'S CORRESPONDING C TO A 3 LETTER CODE FOR EACH COMPONENT USED IN THE DEFINE STATEMENTS C C Soluble Solids, Protein, and Extractives from FEEDPROP DEFINE HCSOL PARAMETER 7 DEFINE HCPRO PARAMETER 8 DEFINE HCEXT PARAMETER 9 F HCCH4 = 52647.46 F HCX2S = 15435. F HCFUR = 20080.2 F HCXMF = 22702.7 F HCAA = 14251.1 F HCCEL = 16458.12 F HCXYN = 16858.11 F HCARN = 16858.11 F HCXNN = 16458.12 F HCGAN = 16458.12 F HCXLG = 24207. F HCACE = 14263.0 F HCEXS = 24207. C ASSUMED UNKNOWN HAD THE SAME HEATING VALUE C AS LIGNIN SINCE IT IS MODELED AS LIGNIN F HCGLO = 14816.06 F HCCLB = 18313.63 F HCXNO = 14816.06 F HCGAO = 14816.06 F HCARO = 14837.0 F HCXYO = 14837.0 F HCTAR = 16642.9 F HCACO = 14263.0 C ASSUMED ACETOLIGOMERS HAD THE SAME HEATING VALUE AS C XYLAN SINCE THAT IS HOW THEY ARE MODELLED F HCXLL = 16444.01 F HCGLU = 14836.8 F HCXYL = 14859.9 F HCXNS = 14836.8 F HCGAL = 14836.8 F HCARA = 14859.9 F HCXLA = 14265.5 F HCCLS = 22632.2 F HCETO = 28140.2 F HCZYM = 20035.5 F HCGLY = 17022.4 F HCSUC = 12090.9 F HCBIO = 21704.0 F HCC = 31200.6 F HCUNK = 13674. F HCACN = 13000. C THIS VALUE IS JUST A PLACEHOLDER UNTIL THE ACTUAL VALUE FOR C AMMONIUM ACETATE CAN BE FOUND. F HCCOI = 37583.3 F HCDEN = 42325.4 F HCXLGS = 24207. C C CALCULATE THE BTU/HR OF STREAM 615, ANAEROBIC OFF-GAS C F BTU615 = CH4615*HCCH4 + X2S615*HCX2S + FUR615*HCFUR + F 1 XMF615*HCXMF + AA615*HCAA F WRITE(NHSTRY,*)'HHV of 615 (Btu/Hr) -- BTU615= ',BTU615 C C Calculate the BTU/HR of stream 101, biomass feed C F BTU101 = CH4101*HCCH4 + F 1 SOL101*HCSOL + CEL101*HCCEL + XYN101*HCXYN + F 2 ARN101*HCARN + XNN101*HCXNN + GAN101*HCGAN + F 3 XLG101*HCXLG + ACE101*HCACE + EXS101*HCEXS + F 4 GLO101*HCGLO + CLB101*HCCLB + XNO101*HCXNO + F 5 GAO101*HCGAO + ARO101*HCARO + XYO101*HCXYO + F 6 TAR101*HCTAR + ACO101*HCACO + FUR101*HCFUR + F 7 XMF101*HCXMF + XLL101*HCXLL + GLU101*HCGLU + F 8 XYL101*HCXYL + XNS101*HCXNS + GAL101*HCGAL + F 9 ARA101*HCARA + AA101*HCAA + XLA101*HCXLA + F * CLS101*HCCLS + ETO101*HCETO + ZYM101*HCZYM + F 1 GLY101*HCGLY + SUC101*HCSUC + BIO101*HCBIO + F 2 C101*HCC + UNK101*HCUNK + X2S101*HCX2S + F 3 ACN101*HCACN + COI101*HCCOI + DEN101*HCDEN + F 4 XSL101*HCXLGS + EXT101*HCEXT + PRO101*HCPRO F WRITE(NHSTRY,*)'HHV of 101 (Btu/Hr) -- BTU101= ',BTU101 C C Calculate the BTU/HR of stream 840, either natural gas or biomass supplement C F BTU840 = CH4840*HCCH4 + F 1 SOL840*HCSOL + CEL840*HCCEL + XYN840*HCXYN + F 2 ARN840*HCARN + XNN840*HCXNN + GAN840*HCGAN + F 3 XLG840*HCXLG + ACE840*HCACE + EXS840*HCEXS + F 4 GLO840*HCGLO + CLB840*HCCLB + XNO840*HCXNO + F 5 GAO840*HCGAO + ARO840*HCARO + XYO840*HCXYO + F 6 TAR840*HCTAR + ACO840*HCACO + FUR840*HCFUR + F 7 XMF840*HCXMF + XLL840*HCXLL + GLU840*HCGLU + F 8 XYL840*HCXYL + XNS840*HCXNS + GAL840*HCGAL + F 9 ARA840*HCARA + AA840*HCAA + XLA840*HCXLA + F * CLS840*HCCLS + ETO840*HCETO + ZYM840*HCZYM + F 1 GLY840*HCGLY + SUC840*HCSUC + BIO840*HCBIO + F 2 C840*HCC + UNK840*HCUNK + X2S840*HCX2S + F 3 ACN840*HCACN + COI840*HCCOI + DEN840*HCDEN + F 4 XSL840*HCXLGS + EXT840*HCEXT + PRO840*HCPRO F WRITE(NHSTRY,*)'HHV of 840 (Btu/Hr) -- BTU840= ',BTU840 C C CALCULATE THE BTU/HR OF STREAM 803, SOLIDS C F BTU803 = SOL803*HCSOL + CEL803*HCCEL + XYN803*HCXYN + F 1 ARN803*HCARN + XNN803*HCXNN + GAN803*HCGAN + F 2 XLG803*HCXLG + ACE803*HCACE + EXS803*HCEXS + F 3 GLO803*HCGLO + CLB803*HCCLB + XNO803*HCXNO + F 4 GAO803*HCGAO + ARO803*HCARO + XYO803*HCXYO + F 5 TAR803*HCTAR + ACO803*HCACO + FUR803*HCFUR + F 6 XMF803*HCXMF + XLL803*HCXLL + GLU803*HCGLU + F 7 XYL803*HCXYL + XNS803*HCXNS + GAL803*HCGAL + F 8 ARA803*HCARA + AA803*HCAA + XLA803*HCXLA + F 9 CLS803*HCCLS + ETO803*HCETO + ZYM803*HCZYM + F * GLY803*HCGLY + SUC803*HCSUC + BIO803*HCBIO + F 1 C803*HCC + UNK803*HCUNK + X2S803*HCX2S + F 2 ACN803*HCACN + COI803*HCCOI + DEN803*HCDEN + F 3 XSL803*HCXLGS + EXT803*HCEXT + PRO803*HCPRO F WRITE(NHSTRY,*)'HHV of 803 (Btu/Hr) -- BTU803= ',BTU803 C C CALCULATE THE BTU/HR OF STREAM 531, SYRUP C F BTU531 = SOL531*HCSOL + CEL531*HCCEL + XYN531*HCXYN + F 1 ARN531*HCARN + XNN531*HCXNN + GAN531*HCGAN + F 2 XLG531*HCXLG + ACE531*HCACE + EXS531*HCEXS + F 3 GLO531*HCGLO + CLB531*HCCLB + XNO531*HCXNO + F 4 GAO531*HCGAO + ARO531*HCARO + XYO531*HCXYO + F 5 TAR531*HCTAR + ACO531*HCACO + FUR531*HCFUR + F 6 XMF531*HCXMF + XLL531*HCXLL + GLU531*HCGLU + F 7 XYL531*HCXYL + XNS531*HCXNS + GAL531*HCGAL + F 8 ARA531*HCARA + AA531*HCAA + XLA531*HCXLA + F 9 CLS531*HCCLS + ETO531*HCETO + ZYM531*HCZYM + F * GLY531*HCGLY + SUC531*HCSUC + BIO531*HCBIO + F 1 C531*HCC + UNK531*HCUNK + X2S531*HCX2S + F 2 ACN531*HCACN + COI531*HCCOI + DEN531*HCDEN + F 3 XSL531*HCXLGS + EXT531*HCEXT + PRO531*HCPRO F WRITE(NHSTRY,*)'HHV of 531 (Btu/Hr) -- BTU531= ',BTU531 C CALCULATE THE TOTAL HEAT INTO THE BOILER (MM BTU/HR) C F BTUTOT = (BTU615+BTU840+BTU803)/1E6 C C CALCULATE % OF HEAT INPUT FOR EACH STREAM C F FRC615 = BTU615/(BTUTOT*1E6) F FRC840 = BTU840/(BTUTOT*1E6) F FRC803 = BTU803/(BTUTOT*1E6) F FRC531 = BTU531/(BTUTOT*1E6) C C WRITE RESULTS TO THE HISTORY FILE C F WRITE(NHSTRY,*)'TOTAL FEED TO BURNER' F WRITE(NHSTRY,*)'BTUTOT (HHV) (MM BTU/HR)= ',BTUTOT F WRITE(NHSTRY,*)'FRC615,FRC840= ',FRC615,FRC840 F WRITE(NHSTRY,*)'FRC803= ',FRC803 F WRITE(NHSTRY,*)'FRC531= ',FRC531 EXECUTE BEFORE M803CMB ; FORTRAN COMBHET2 ; Mark Ruth 2 Nov 98 ; To replace COMBHEAT ; DEFINE HLETOT PARAMETER 2 DEFINE WATCON PARAMETER 3 c Samples Molecular Weights and Lower Heating Values (J/Kmol) for each c component : Each component gets a 3 letter code c Glucose = GLU DEFINE WMLGLU UNARY-PARAM VARIABLE=MW ID1=GLUCOSE ID2=1 DEFINE CMBGLU UNARY-PARAM VARIABLE=HCOM ID1=GLUCOSE ID2=1 c Xylose = XYL DEFINE WMLXYL UNARY-PARAM VARIABLE=MW ID1=XYLOSE ID2=1 ; DEFINE CMBXYL UNARY-PARAM VARIABLE=HCOM ID1=XYLOSE ID2=1 ; Unary-Param was not available, so it is input F CMBXYL = -2.12644E9 c Soluble Solids = SOL DEFINE WMLSOL UNARY-PARAM VARIABLE=MW ID1=SOLSLDS ID2=1 ; LHV calculated by FEEDPROP DEFINE CMBSOL PARAMETER 10 c Arabinose = ARA DEFINE WMLARA UNARY-PARAM VARIABLE=MW ID1=ARABINOS ID2=1 ; DEFINE CMBARA UNARY-PARAM VARIABLE=HCOM ID1=ARABINOS ID2=1 ; Unary-Param was not available, so it is input F CMBARA = -2.12644E9 c Galactose = GAL DEFINE WMLGAL UNARY-PARAM VARIABLE=MW ID1=GALACTOS ID2=1 ; DEFINE CMBGAL UNARY-PARAM VARIABLE=HCOM ID1=GALACTOS ID2=1 ; Unary-Param was incorrect, so it is input F CMBGAL = -2.54735E9 c Mannose = XNS DEFINE WMLXNS UNARY-PARAM VARIABLE=MW ID1=MANNOSE ID2=1 ; DEFINE CMBXNS UNARY-PARAM VARIABLE=HCOM ID1=MANNOSE ID2=1 ; Unary-Param was incorrect, so it is input F CMBXNS = -2.54735E9 c Glucolig = GLO DEFINE WMLGLO UNARY-PARAM VARIABLE=MW ID1=GLUCOLIG ID2=1 ; DEFINE CMBGLO UNARY-PARAM VARIABLE=HCOM ID1=GLUCOLIG ID2=1 ; Unary-Param was incorrect, so it is input F CMBGLO = -2.30664E9 c Cellobiose = CLB DEFINE WMLCLB UNARY-PARAM VARIABLE=MW ID1=CELLOB ID2=1 ; DEFINE CMBCLB UNARY-PARAM VARIABLE=HCOM ID1=CELLOB ID2=1 ; Unary-Param was incorrect, so it is input F CMBCLB = -6.11137E9 c Xylolig = XYO DEFINE WMLXYO UNARY-PARAM VARIABLE=MW ID1=XYLOLIG ID2=1 ; DEFINE CMBXYO UNARY-PARAM VARIABLE=HCOM ID1=XYLOLIG ID2=1 ; Unary-Param was not available, so it is input ;BGA edit, 6/17/02 Changed LHV to reflect those in energy bal model ;F CMBXYO = -1.88574E9 F CMBXYO = -1846102716 c Manolig = XNO DEFINE WMLXNO UNARY-PARAM VARIABLE=MW ID1=MANOLIG ID2=1 ; DEFINE CMBXNO UNARY-PARAM VARIABLE=HCOM ID1=MANOLIG ID2=1 ; Unary-Param was incorrect, so it is input F CMBXNO = -2.30664E9 c Galaolig = GAO DEFINE WMLGAO UNARY-PARAM VARIABLE=MW ID1=GALAOLIG ID2=1 ; DEFINE CMBGAO UNARY-PARAM VARIABLE=HCOM ID1=GALAOLIG ID2=1 ; Unary-Param was incorrect, so it is input F CMBGAO = -2.30664E9 c Arabolig = ARO DEFINE WMLARO UNARY-PARAM VARIABLE=MW ID1=ARABOLIG ID2=1 ; DEFINE CMBARO UNARY-PARAM VARIABLE=HCOM ID1=ARABOLIG ID2=1 ; Unary-Param was not available, so it is input ;BGA edit, 6/17/02 Changed LHV to reflect those in energy bal model ;F CMBXYO = -1.88574E9 F CMBXYO = -1.84610E9 c Xylitol = XLL DEFINE WMLXLL UNARY-PARAM VARIABLE=MW ID1=XYLITOL ID2=1 ; DEFINE CMBXLL UNARY-PARAM VARIABLE=HCOM ID1=XYLITOL ID2=1 ; Unary-Param was not available, so it is input ; BGA Edit, 6/17/02, Changed LHV to reflect value in energy bal ;F CMBXLL = -2.36706E9 F CMBXLL = -3.33847E9 c Ethanol = ETH DEFINE WMLETH UNARY-PARAM VARIABLE=MW ID1=ETHANOL ID2=1 DEFINE CMBETH UNARY-PARAM VARIABLE=HCOM ID1=ETHANOL ID2=1 c Furfural = FUR DEFINE WMLFUR UNARY-PARAM VARIABLE=MW ID1=FURFURAL ID2=1 ; DEFINE CMBFUR UNARY-PARAM VARIABLE=HCOM ID1=FURFURAL ID2=1 ; Unary-Param incorrect, so it is input ; BGA Edit, 6/17/02, Changed LHV to reflect value in energy bal ;F CMBFUR = -1.94377E9 F CMBFUR = -2.25104E9 c HMF = XMF DEFINE WMLXMF UNARY-PARAM VARIABLE=MW ID1=HMF ID2=1 ; DEFINE CMBXMF UNARY-PARAM VARIABLE=HCOM ID1=HMF ID2=1 ; Unary-Param incorrect, so it is input ; BGA Edit, 6/17/02, Changed LHV to reflect value in energy bal ;F CMBXMF = -2.88303E9 F CMBXMF = -2.93021E9 c CH4 = CH4 DEFINE WMLCH4 UNARY-PARAM VARIABLE=MW ID1=CH4 ID2=1 DEFINE CMBCH4 UNARY-PARAM VARIABLE=HCOM ID1=CH4 ID2=1 c Lactic Acid = XLA DEFINE WMLXLA UNARY-PARAM VARIABLE=MW ID1=LACID ID2=1 DEFINE CMBXLA UNARY-PARAM VARIABLE=HCOM ID1=LACID ID2=1 c Acetic Acid = AAC DEFINE WMLAAC UNARY-PARAM VARIABLE=MW ID1=AACID ID2=1 DEFINE CMBAAC UNARY-PARAM VARIABLE=HCOM ID1=AACID ID2=1 c NH4ACET = ACN DEFINE WMLACN UNARY-PARAM VARIABLE=MW ID1=NH4ACET ID2=1 DEFINE CMBACN UNARY-PARAM VARIABLE=HCOM ID1=NH4ACET ID2=1 c GLYCEROL = GLY DEFINE WMLGLY UNARY-PARAM VARIABLE=MW ID1=GLYCEROL ID2=1 DEFINE CMBGLY UNARY-PARAM VARIABLE=HCOM ID1=GLYCEROL ID2=1 c Succinic Acid = SUC DEFINE WMLSUC UNARY-PARAM VARIABLE=MW ID1=SUCCACID ID2=1 DEFINE CMBSUC UNARY-PARAM VARIABLE=HCOM ID1=SUCCACID ID2=1 c Oil = COI DEFINE WMLCOI UNARY-PARAM VARIABLE=MW ID1=OIL ID2=1 DEFINE CMBCOI UNARY-PARAM VARIABLE=HCOM ID1=OIL ID2=1 c Acetolig = ACO DEFINE WMLACO UNARY-PARAM VARIABLE=MW ID1=ACETOLIG ID2=1 ; DEFINE CMBACO UNARY-PARAM VARIABLE=HCOM ID1=ACETOLIG ID2=1 ; Unary-Param was not available, so it is input ; BGA Edit, 6/18/02, Changed LHV to reflect value in energy bal ;F CMBACO = -2.24039E8 F CMBACO = -8.14154E8 c Unknown = UNK DEFINE WMLUNK UNARY-PARAM VARIABLE=MW ID1=UNKNOWN ID2=1 ; DEFINE CMBUNK UNARY-PARAM VARIABLE=HCOM ID1=UNKNOWN ID2=1 ; Unary-Param was not available, so it is input ; BGA Edit, 6/18/02, Changed LHV to reflect value in energy bal ;F CMBUNK = -3.928E9 F CMBUNK = -1.94411E8 c H2S = X2S DEFINE WMLX2S UNARY-PARAM VARIABLE=MW ID1=H2S ID2=1 DEFINE CMBX2S UNARY-PARAM VARIABLE=HCOM ID1=H2S ID2=1 c Denaturant = DEN DEFINE WMLDEN UNARY-PARAM VARIABLE=MW ID1=DENAT ID2=1 DEFINE CMBDEN UNARY-PARAM VARIABLE=HCOM ID1=DENAT ID2=1 c Cellulose = CEL DEFINE WMLCEL UNARY-PARAM VARIABLE=MW ID1=CELLULOS ID2=1 ; DEFINE CMBCEL UNARY-PARAM VARIABLE=HCOM ID1=CELLULOS ID2=1 ; Unary-Param was not available, so it is input F CMBCEL = -2.58778E9 c Xylan = XYN DEFINE WMLXYN UNARY-PARAM VARIABLE=MW ID1=XYLAN ID2=1 ; DEFINE CMBXYN UNARY-PARAM VARIABLE=HCOM ID1=XYLAN ID2=1 ; Unary-Param incorrect, so it is input F CMBXYN = -2.16759E9 c Lignin = XLG DEFINE WMLXLG UNARY-PARAM VARIABLE=MW ID1=LIGNIN ID2=1 ; DEFINE CMBXLG UNARY-PARAM VARIABLE=HCOM ID1=LIGNIN ID2=1 ; Unary-Param was not available, so it is input ; BGA Edit, 6/18/02, Changed LHV to reflect value in energy bal ;F CMBXLG = -3.928E9 F CMBXLG = -3.65074E9 c Cellulase = CLS DEFINE WMLCLS UNARY-PARAM VARIABLE=MW ID1=CELLULAS ID2=1 ; DEFINE CMBCLS UNARY-PARAM VARIABLE=HCOM ID1=CELLULAS ID2=1 ; Unary-Param was not available, so it is input F CMBCLS = -5.09527E8 c Biomass = BIO DEFINE WMLBIO UNARY-PARAM VARIABLE=MW ID1=BIOMASS ID2=1 ; DEFINE CMBBIO UNARY-PARAM VARIABLE=HCOM ID1=BIOMASS ID2=1 ; Unary-Param was not available, so it is input F CMBBIO = -4.94720E8 c Zymo = ZYM DEFINE WMLZYM UNARY-PARAM VARIABLE=MW ID1=ZYMO ID2=1 ; DEFINE CMBZYM UNARY-PARAM VARIABLE=HCOM ID1=ZYMO ID2=1 ; Unary-Param was not available, so it is input F CMBZYM = -4.79563E8 c Arabinan = ARN DEFINE WMLARN UNARY-PARAM VARIABLE=MW ID1=ARABINAN ID2=1 ; DEFINE CMBARN UNARY-PARAM VARIABLE=HCOM ID1=ARABINAN ID2=1 ; Unary-Param incorrect, so it is input F CMBARN = -2.16759E9 c Mannan = XNN DEFINE WMLXNN UNARY-PARAM VARIABLE=MW ID1=MANNAN ID2=1 ; DEFINE CMBXNN UNARY-PARAM VARIABLE=HCOM ID1=MANNAN ID2=1 ; Unary-Param was not available, so it is input F CMBXNN = -2.58778E9 c Galactan = GAN DEFINE WMLGAN UNARY-PARAM VARIABLE=MW ID1=GALACTAN ID2=1 ; DEFINE CMBGAN UNARY-PARAM VARIABLE=HCOM ID1=GALACTAN ID2=1 ; Unary-Param was not available, so it is input F CMBGAN = -2.58778E9 c Tar = TAR DEFINE WMLTAR UNARY-PARAM VARIABLE=MW ID1=TAR ID2=1 ; DEFINE CMBTAR UNARY-PARAM VARIABLE=HCOM ID1=TAR ID2=1 ; Unary-Param incorrect, so it is input F CMBTAR = -2.40814E9 c Acetate = ACE DEFINE WMLACE UNARY-PARAM VARIABLE=MW ID1=ACETATE ID2=1 ; DEFINE CMBACE UNARY-PARAM VARIABLE=HCOM ID1=ACETATE ID2=1 ; Unary-Param incorrect, so it is input ; BGA Edit, 6/18/02, Changed LHV to reflect value in energy bal ;F CMBACE = -7.6988E8 F CMBACE = -8.1407E8 c C = C DEFINE WMLC UNARY-PARAM VARIABLE=MW ID1=C ID2=1 ; DEFINE CMBC UNARY-PARAM VARIABLE=HCOM ID1=C ID2=1 ; BGA, 6/18/02, Unary-Param was incorrect, so it is input F CMBC = -1.0265E9 c Soluble Lignin = SLG DEFINE WMLSLG UNARY-PARAM VARIABLE=MW ID1=LIGNIN ID2=1 ; DEFINE CMBSLG UNARY-PARAM VARIABLE=HCOM ID1=LIGNIN ID2=1 ; Unary-Param was not available, so it is input ; BGA Edit, 6/18/02, Changed LHV to reflect value in energy bal ;F CMBSLG = -8.397E9 F CMBSLG = -3.64655E9 c Extractives = EXT DEFINE WMLEXT UNARY-PARAM VARIABLE=MW ID1=EXTRACT ID2=1 ; LHV calculated by FEEDPROP DEFINE CMBEXT PARAMETER 11 c Protein = PRO DEFINE WMLPRO UNARY-PARAM VARIABLE=MW ID1=PROTEIN ID2=1 ; LHV calculated by FEEDPROP DEFINE CMBPRO PARAMETER 12 ; Water for MW calculation purposes DEFINE WMLH2O UNARY-PARAM VARIABLE=MW ID1=H2O ID2=1 ; c The heat of vaporization of water is 2442.5 kJ/kg at 25C c The molecular weight of water is 18.01528 1st Student Edition c VAPWAT is the heat of vaporization of water in J/Kmol F VAPWAT = 2442.5 * 1000 * 18.01528 ; c The following are test write statements that show the values c the lower heating value of methane is 802620000 J/Kmol c the lower heating value of ethanol is 1235000000 J/Kmol F WRITE(NHSTRY,*)'MW CH4=',WMLCH4 F WRITE(NHSTRY,*)'HEAT OF COMB CH4 (J/kmol)=',CMBCH4 F WRITE(NHSTRY,*)'MW ETHANOL=',WMLETH F WRITE(NHSTRY,*)'HEAT OF COMB ETHANOL=',CMBETH c More Tests F WRITE(NHSTRY,*)'MW GLU=',WMLGLU F WRITE(NHSTRY,*)'HEAT OF COMB GLU=',CMBGLU F WRITE(NHSTRY,*)'MW XYL=',WMLXYL F WRITE(NHSTRY,*)'HEAT OF COMB XYL=',CMBXYL F WRITE(NHSTRY,*)'MW SOL=',WMLSOL F WRITE(NHSTRY,*)'HEAT OF COMB SOL=',CMBSOL F WRITE(NHSTRY,*)'MW ARA=',WMLARA F WRITE(NHSTRY,*)'HEAT OF COMB ARA=',CMBARA F WRITE(NHSTRY,*)'MW GAL=',WMLGAL F WRITE(NHSTRY,*)'HEAT OF COMB GAL=',CMBGAL F WRITE(NHSTRY,*)'MW XNS=',WMLXNS F WRITE(NHSTRY,*)'HEAT OF COMB XNS=',CMBXNS F WRITE(NHSTRY,*)'MW GLO=',WMLGLO F WRITE(NHSTRY,*)'HEAT OF COMB GLO=',CMBGLO F WRITE(NHSTRY,*)'MW CLB=',WMLCLB F WRITE(NHSTRY,*)'HEAT OF COMB CLB=',CMBCLB F WRITE(NHSTRY,*)'MW XYO=',WMLXYO F WRITE(NHSTRY,*)'HEAT OF COMB XYO=',CMBXYO F WRITE(NHSTRY,*)'MW XNO=',WMLXNO F WRITE(NHSTRY,*)'HEAT OF COMB XNO=',CMBXNO F WRITE(NHSTRY,*)'MW GAO=',WMLGAO F WRITE(NHSTRY,*)'HEAT OF COMB GAO=',CMBGAO F WRITE(NHSTRY,*)'MW ARO=',WMLARO F WRITE(NHSTRY,*)'HEAT OF COMB ARO=',CMBARO F WRITE(NHSTRY,*)'MW XLL=',WMLXLL F WRITE(NHSTRY,*)'HEAT OF COMB XLL=',CMBXLL F WRITE(NHSTRY,*)'MW FUR=',WMLFUR F WRITE(NHSTRY,*)'HEAT OF COMB FUR=',CMBFUR F WRITE(NHSTRY,*)'MW XMF=',WMLXMF F WRITE(NHSTRY,*)'HEAT OF COMB XMF=',CMBXMF F WRITE(NHSTRY,*)'MW XLA=',WMLXLA F WRITE(NHSTRY,*)'HEAT OF COMB XLA=',CMBXLA F WRITE(NHSTRY,*)'MW AAC=',WMLAAC F WRITE(NHSTRY,*)'HEAT OF COMB AAC=',CMBAAC F WRITE(NHSTRY,*)'MW GLY=',WMLGLY F WRITE(NHSTRY,*)'HEAT OF COMB GLY=',CMBGLY F WRITE(NHSTRY,*)'MW SUC=',WMLSUC F WRITE(NHSTRY,*)'HEAT OF COMB SUC=',CMBSUC F WRITE(NHSTRY,*)'MW COI=',WMLCOI F WRITE(NHSTRY,*)'HEAT OF COMB COI=',CMBCOI F WRITE(NHSTRY,*)'MW ACO=',WMLACO F WRITE(NHSTRY,*)'HEAT OF COMB ACO=',CMBACO F WRITE(NHSTRY,*)'MW UNK=',WMLUNK F WRITE(NHSTRY,*)'HEAT OF COMB UNK=',CMBUNK F WRITE(NHSTRY,*)'MW X2S=',WMLX2S F WRITE(NHSTRY,*)'HEAT OF COMB X2S=',CMBX2S F WRITE(NHSTRY,*)'MW DEN=',WMLDEN F WRITE(NHSTRY,*)'HEAT OF COMB DEN=',CMBDEN F WRITE(NHSTRY,*)'MW CEL=',WMLCEL F WRITE(NHSTRY,*)'HEAT OF COMB CEL=',CMBCEL F WRITE(NHSTRY,*)'MW XYN=',WMLXYN F WRITE(NHSTRY,*)'HEAT OF COMB XYN=',CMBXYN F WRITE(NHSTRY,*)'MW XLG=',WMLXLG F WRITE(NHSTRY,*)'HEAT OF COMB XLG=',CMBXLG F WRITE(NHSTRY,*)'MW CLS=',WMLCLS F WRITE(NHSTRY,*)'HEAT OF COMB CLS=',CMBCLS F WRITE(NHSTRY,*)'MW BIO=',WMLBIO F WRITE(NHSTRY,*)'HEAT OF COMB BIO=',CMBBIO F WRITE(NHSTRY,*)'MW ZYM=',WMLZYM F WRITE(NHSTRY,*)'HEAT OF COMB ZYM=',CMBZYM F WRITE(NHSTRY,*)'MW ARN=',WMLARN F WRITE(NHSTRY,*)'HEAT OF COMB ARN=',CMBARN F WRITE(NHSTRY,*)'MW XNN=',WMLXNN F WRITE(NHSTRY,*)'HEAT OF COMB XNN=',CMBXNN F WRITE(NHSTRY,*)'MW GAN=',WMLGAN F WRITE(NHSTRY,*)'HEAT OF COMB GAN=',CMBGAN F WRITE(NHSTRY,*)'MW TAR=',WMLTAR F WRITE(NHSTRY,*)'HEAT OF COMB TAR=',CMBTAR F WRITE(NHSTRY,*)'MW ACE=',WMLACE F WRITE(NHSTRY,*)'HEAT OF COMB ACE=',CMBACE F WRITE(NHSTRY,*)'MW C=',WMLC F WRITE(NHSTRY,*)'HEAT OF COMB C=',CMBC F WRITE(NHSTRY,*)'MW Soluble Lignin=',WMLSLG F WRITE(NHSTRY,*)'HEAT OF COMB Soluble Lignin=',CMBSLG F WRITE(NHSTRY,*)'MW Extractives=',WMLEXT F WRITE(NHSTRY,*)'HEAT OF COMB Extractives=',CMBEXT F WRITE(NHSTRY,*)'MW Protein=',WMLPRO F WRITE(NHSTRY,*)'HEAT OF COMB Protein=',CMBPRO F WRITE(NHSTRY,*)'MW H2O=',WMLH2O ; c Following is the calulation of LHV for stream 615 DEFINE ETH615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE FUR615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=HMF DEFINE CH4615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE AAC615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=AACID DEFINE X2S615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=H2S DEFINE WAT615 MOLE-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=H2O DEFINE FLW615 STREAM-VAR STREAM=615 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW c VLW615 calculates the lower heating value in J/hr c Water entering the burner is not included in this calculation, c because it is already a vapor F VLW615 = ETH615 * CMBETH + FUR615 * CMBFUR F 1 + XMF615 * CMBXMF + CH4615 * CMBCH4 F 2 + AAC615 * CMBAAC + X2S615 * CMBX2S ; the following line could be used to include water if desired ; BGA EDIT, 6/18/02, CHANGED TO + BECAUSE HEATS OF COMB WERE MODELED AS NEG. ; F 9 + WAT615 * VAPWAT c HLV615 calculates the lower heating value in J/kg F HLV615 = VLW615 / FLW615 c HLE615 calculates the lower heating value in Btu/lb c Conversion Factors 9.478E-4 Btu/J & 2.20462 lb/kg F HLE615 = HLV615 * 9.478E-4 / 2.20462 ; F WRITE(NHSTRY,*)'LHV OF 615 (J/HR)=',VLW615 F WRITE(NHSTRY,*)'LHV OF 615 (J/KG)=',HLV615 F WRITE(NHSTRY,*)'LHV OF 615 (BTU/LB)=',HLE615 ; c Following is the calculation of LHV for stream 803 DEFINE WAT803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=H2O DEFINE GLU803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE SOL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE ARA803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE GAL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE XNS803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GLO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XYO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE XNO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XLL803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE ETH803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE FUR803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=HMF DEFINE CH4803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE XLA803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=LACID DEFINE AAC803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=AACID DEFINE ACN803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE GLY803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE COI803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=OIL DEFINE ACO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE UNK803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=H2S DEFINE DEN803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE SLG803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO803 MOLE-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=PROTEIN DEFINE CEL803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE XLG803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE CLS803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=CELLULAS DEFINE BIO803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE ZYM803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE ARN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE TAR803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACE803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE C803 MOLE-FLOW STREAM=803 SUBSTREAM=CISOLID COMPONENT=C DEFINE FLW83M STREAM-VAR STREAM=803 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FLW83C STREAM-VAR STREAM=803 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW c VLW803 calculates the lower heating value in J/hr F VLW803 = GLU803 * CMBGLU + XYL803 * CMBXYL F 1 + SOL803 * CMBSOL + ARA803 * CMBARA F 2 + GAL803 * CMBGAL + XNS803 * CMBXNS F 3 + GLO803 * CMBGLO + CLB803 * CMBCLB F 4 + XYO803 * CMBXYO + XNO803 * CMBXNO F 5 + GAO803 * CMBGAO + ARO803 * CMBARO F 6 + XLL803 * CMBXLL + ETH803 * CMBETH F 7 + FUR803 * CMBFUR + XMF803 * CMBXMF F 8 + CH4803 * CMBCH4 + XLA803 * CMBXLA F 9 + AAC803 * CMBAAC + ACN803 * CMBACN F 1 + GLY803 * CMBGLY + SUC803 * CMBSUC F 2 + COI803 * CMBCOI + ACO803 * CMBACO F 3 + UNK803 * CMBUNK + X2S803 * CMBX2S F 4 + DEN803 * CMBDEN + SLG803 * CMBSLG F 5 + EXT803 * CMBEXT + PRO803 * CMBPRO F 6 + CEL803 * CMBCEL F 5 + XYN803 * CMBXYN + XLG803 * CMBXLG F 6 + CLS803 * CMBCLS + BIO803 * CMBBIO F 7 + ZYM803 * CMBZYM + ARN803 * CMBARN F 8 + XNN803 * CMBXNN + GAN803 * CMBGAN F 9 + TAR803 * CMBTAR + ACE803 * CMBACE F 1 + C803 * CMBC ; BGA EDIT, 6/18/02, CHANGED TO + BECAUSE HEATS OF COMB WERE MODELED AS NEG. F 9 + WAT803 * VAPWAT c HLV803 calculates the lower heating value in J/kg F HLV803 = VLW803 / (FLW83M + FLW83C) c HLE803 calculates the lower heating value in Btu/lb c Conversion Factors 9.478E-4 Btu/J & 2.20462 lb/kg F HLE803 = HLV803 * 9.478E-4 / 2.20462 ; F WRITE(NHSTRY,*)'LHV OF 803 (J/HR)=',VLW803 F WRITE(NHSTRY,*)'LHV OF 803 (J/KG)=',HLV803 F WRITE(NHSTRY,*)'LHV OF 803 (BTU/LB)=',HLE803 ; ; c Following is the calculation of LHV for stream 840 DEFINE WAT840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=H2O DEFINE GLU840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLUCOSE DEFINE XYL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLOSE DEFINE SOL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=SOLSLDS DEFINE ARA840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ARABINOS DEFINE GAL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GALACTOS DEFINE XNS840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=MANNOSE DEFINE GLO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLUCOLIG DEFINE CLB840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CELLOB DEFINE XYO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLOLIG DEFINE XNO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=MANOLIG DEFINE GAO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GALAOLIG DEFINE ARO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ARABOLIG DEFINE XLL840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=XYLITOL DEFINE ETH840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ETHANOL DEFINE FUR840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=FURFURAL DEFINE XMF840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=HMF DEFINE CH4840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=CH4 DEFINE XLA840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=LACID DEFINE AAC840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=AACID DEFINE ACN840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=NH4ACET DEFINE GLY840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=GLYCEROL DEFINE SUC840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=SUCCACID DEFINE COI840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=OIL DEFINE ACO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=ACETOLIG DEFINE UNK840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=UNKNOWN DEFINE X2S840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=H2S DEFINE DEN840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=DENAT DEFINE SLG840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=LGNSOL DEFINE EXT840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=EXTRACT DEFINE PRO840 MOLE-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=PROTEIN DEFINE CEL840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=CELLULOS DEFINE XYN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=XYLAN DEFINE XLG840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=LIGNIN DEFINE CLS840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=CELLULAS DEFINE BIO840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=BIOMASS DEFINE ZYM840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ZYMO DEFINE ARN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ARABINAN DEFINE XNN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=MANNAN DEFINE GAN840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=GALACTAN DEFINE TAR840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=TAR DEFINE ACE840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=ACETATE DEFINE C840 MOLE-FLOW STREAM=840 SUBSTREAM=CISOLID COMPONENT=C DEFINE FL840M STREAM-VAR STREAM=840 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE FL840C STREAM-VAR STREAM=840 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW c VLW840 calculates the lower heating value in J/hr F VLW840 = GLU840 * CMBGLU + XYL840 * CMBXYL F 1 + SOL840 * CMBSOL + ARA840 * CMBARA F 2 + GAL840 * CMBGAL + XNS840 * CMBXNS F 3 + GLO840 * CMBGLO + CLB840 * CMBCLB F 4 + XYO840 * CMBXYO + XNO840 * CMBXNO F 5 + GAO840 * CMBGAO + ARO840 * CMBARO F 6 + XLL840 * CMBXLL + ETH840 * CMBETH F 7 + FUR840 * CMBFUR + XMF840 * CMBXMF F 8 + CH4840 * CMBCH4 + XLA840 * CMBXLA F 9 + AAC840 * CMBAAC + ACN840 * CMBACN F 1 + GLY840 * CMBGLY + SUC840 * CMBSUC F 2 + COI840 * CMBCOI + ACO840 * CMBACO F 3 + UNK840 * CMBUNK + X2S840 * CMBX2S F 4 + DEN840 * CMBDEN + SLG840 * CMBSLG F 5 + EXT840 * CMBEXT + PRO840 * CMBPRO F 6 + CEL840 * CMBCEL F 5 + XYN840 * CMBXYN + XLG840 * CMBXLG F 6 + CLS840 * CMBCLS + BIO840 * CMBBIO F 7 + ZYM840 * CMBZYM + ARN840 * CMBARN F 8 + XNN840 * CMBXNN + GAN840 * CMBGAN F 9 + TAR840 * CMBTAR + ACE840 * CMBACE F 1 + C840 * CMBC ; BGA EDIT, 6/18/02, CHANGED TO + BECAUSE HEATS OF COMB WERE MODELED AS NEG. F 9 + WAT840 * VAPWAT c HLV840 calculates the lower heating value in J/kg F FLW840 = FL840M + FL840C F HLV840 = VLW840 / FLW840 C HLE840 calculates the lower heating value in Btu/lb C Conversion Factors 9.478E-4 Btu/J & 2.20462 lb/kg F HLE840 = HLV840 * 9.478E-4 / 2.20462 ; F WRITE(NHSTRY,*)'LHV OF 840 (J/HR)=',VLW840 F WRITE(NHSTRY,*)'LHV OF 840 (J/KG)=',HLV840 F WRITE(NHSTRY,*)'LHV OF 840 (BTU/LB)=',HLE840 ; ; VLWTOT calculates the sum of the lower heating values of the 3 streams F VLWTOT = VLW615 + VLW803 + VLW840 ; HVLTOT calculates the lower heating value in J/kg F HLVTOT = VLWTOT / (FLW615 + FLW83M + FLW83C + FLW840) c HLETOT calculates the lower heating value in Btu/lb c Conversion Factors 9.478E-4 Btu/J & 2.20462 lb/kg F HLETOT = HLVTOT * 9.478E-4 / 2.20462 ; F WRITE(NHSTRY,*)'TOTAL LHV (J/HR)=',VLWTOT F WRITE(NHSTRY,*)'TOTAL LHV (J/KG)=',HLVTOT F WRITE(NHSTRY,*)'TOTAL LHV (BTU/LB)=',HLETOT ; c WATCON is the water concentration in the boiler feedstreams DEFINE WT615B MASS-FLOW STREAM=615 SUBSTREAM=MIXED COMPONENT=H2O DEFINE WT803B MASS-FLOW STREAM=803 SUBSTREAM=MIXED COMPONENT=H2O DEFINE WT840B MASS-FLOW STREAM=840 SUBSTREAM=MIXED COMPONENT=H2O F WATCON = (WT615B + WT803B + WT840B) / F 1 (FLW615 + FLW83M + FLW83C + FLW840) F WRITE(NHSTRY,*)'WATER CONCENTRATION IN FEEDS TO BURNER=',WATCON READ-VARS WMLGLU CMBGLU WMLXYL WMLSOL & WMLARA WMLGAL WMLXNS & WMLGLO WMLCLB WMLXYO & WMLXNO WMLGAO WMLARO & WMLXLL WMLETH CMBETH WMLFUR & WMLXMF WMLCH4 CMBCH4 WMLXLA CMBXLA WMLAAC CMBAAC & WMLACN CMBACN WMLGLY CMBGLY WMLSUC CMBSUC & WMLCOI CMBCOI WMLACO WMLUNK & WMLX2S CMBX2S WMLDEN CMBDEN WMLCEL & WMLXYN WMLXLG WMLCLS & WMLBIO WMLZYM WMLARN & WMLXNN WMLGAN WMLTAR & WMLACE WMLC & ETH615 FUR615 XMF615 CH4615 AAC615 X2S615 WAT615 & FLW615 & GLU803 XYL803 SOL803 ARA803 GAL803 XNS803 GLO803 & CLB803 XYO803 XNO803 GAO803 ARO803 XLL803 ETH803 & FUR803 XMF803 CH4803 XLA803 AAC803 ACN803 GLY803 & SUC803 COI803 ACO803 UNK803 X2S803 DEN803 CEL803 & XYN803 XLG803 CLS803 BIO803 ZYM803 ARN803 XNN803 & GAN803 TAR803 ACE803 C803 FLW83M FLW83C & CH4840 WT615B WT803B CMBSOL WRITE-VARS HLETOT WATCON ; ; ; FORTRAN DEWPT DEFINE ACIDFR MOLE-FRAC STREAM=804D SUBSTREAM=MIXED COMPONENT=H2SO4 DEFINE H2OFR MOLE-FRAC STREAM=804D SUBSTREAM=MIXED COMPONENT=H2O DEFINE PRES STREAM-VAR STREAM=804D SUBSTREAM=MIXED VARIABLE=PRES DEFINE TOUT BLOCK-VAR BLOCK=H801+ VARIABLE=TEMP SENTENCE=PARAM C C THE ACID DEW POINT OF THE FLUE GAS IS CALCULATED C FROM THE FOLLOWING EQUATION THAT WAS TAKEN FROM C HYDROCARBON PROCESSING, FEBRUARY 1993, GANAPATHY, V. C "COMPUTE DEW POINT OF GASES". C C THE MOLE FRACTIONS OF H2O AND H2SO4 ARE ASSUMED C TO BE EQUIVALENT TO THEIR PARTIAL PRESSURES C F HGPRES = PRES*760.0 C HGPRES IS THE PRESSURE IN MM HG F IF (ACIDFR .LT. 1E-12) THEN F TDP = 433 F ELSE F TDPINV = (2.276E-3)-2.943E-5*LOG(H2OFR*HGPRES) - F 1 8.58E-5*LOG(ACIDFR*HGPRES) + F 2 6.2E-6*LOG(H2OFR*HGPRES)*LOG(ACIDFR*HGPRES) F END IF C C THE ACID DEW POINT IS THE INVERSE OF THE VALUE CALCULATED C F TDP = 1.0/TDPINV C C WRITE THE ANSWERS TO THE HISTORY FILE. C F WRITE(NHSTRY,*)'THE ACID DEW POINT IS= ',TDP, 'K' F WRITE(NHSTRY,*)'PRES,H2OFR,ACIDFR= ',PRES,H2OFR,ACIDFR F TDPC = TDP - 273.2 F TEXIT = TDPC + 34.7 C C THE AIR PREHEATER EXIT TEMPERATURE SHOULD HAVE A 50-75 F C SAFETY FACTOR. THE AVERAGE IS 62.5 F (34.7 C) C C CHECK TO SEE IF TEXIT IS BELOW AIR PREHEATER EXIT C TEMPERATURE. IF IT IS, THEN LEAVE THE AIR PREHEATER TEMPERATURE C IF NOT, THEN SET THE AIR PREHEATER TEMPERATURE EQUAL TO THE C TEXIT C F IF (TEXIT .GT. 149.) THEN F TOUT = TEXIT F ELSE F TOUT=149. F END IF READ-VARS ACIDFR H2OFR PRES WRITE-VARS TOUT ; FORTRAN EFFCY F COMMON / HEATIN / BTUTOT F COMMON / EFFCYS /HTRATE, BLREFF DEFINE WKOUT INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WTOTAL DEFINE QSTEAM INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QBOILER C CALCULATE THE HEAT RATE(BTU/KWH) C F HTRATE = (BTUTOT*1.E6)/(-WKOUT) F WRITE(NHSTRY,*)'HTRATE,BTUTOT,WKOUT= ',HTRATE,BTUTOT,WKOUT C C CALCULATE THE BOILER EFFICIENCY C F BLRBTU = QSTEAM*3600.*3.968E-3 C BLRBTU IS THE HEAT FROM THE BOILER IN BTU/HR C AND IS CONVERTED FROM CAL/S C 3600 S/H AND 3.968E-3 BTU/CAL C F BLREFF = BLRBTU/(BTUTOT*1.E6) F WRITE(NHSTRY,*)'BLREFF,BLRBTU,BTUTOT= ',BLREFF,BLRBTU,BTUTOT READ-VARS WKOUT QSTEAM ; FORTRAN MOISTURE DEFINE W803 MASS-FLOW STREAM=803 SUBSTREAM=MIXED & COMPONENT=H2O DEFINE X803 STREAM-VAR STREAM=803 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE C803 STREAM-VAR STREAM=803 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE W615 MASS-FLOW STREAM=615 SUBSTREAM=MIXED & COMPONENT=H2O DEFINE X615 STREAM-VAR STREAM=615 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE C615 STREAM-VAR STREAM=615 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE TOTWAT PARAMETER 51 DEFINE WATPER PARAMETER 52 F TOTWAT = W803 + W615 F TOTFLO = X803 + X615 + C803 + C615 F WATPER = TOTWAT/TOTFLO*100. F WRITE(NHSTRY,*)'WATPER = ',WATPER READ-VARS W803 X803 C803 W615 X615 C615 WRITE-VARS TOTWAT WATPER ; FORTRAN POLLUTE F COMMON / HEATIN / BTUTOT DEFINE FINNOX BLOCK-VAR BLOCK=M803CMB VARIABLE=EXTENT & SENTENCE=EXTENT ID1=67 DEFINE WTNOX UNARY-PARAM VARIABLE=MW ID1=NO2 ID2=1 DEFINE WTCO UNARY-PARAM VARIABLE=MW ID1=CO ID2=1 DEFINE FINCO BLOCK-VAR BLOCK=M803CMB VARIABLE=EXTENT & SENTENCE=EXTENT ID1=40 C SET THE EXPECTED NOX GENERATION RATE, GENNOX (LB/MMBTU) C F GENNOX = 0.20 C 0.2 assumes no NOx control in the burner; from Foster Wheeler C from REI subcontract, 1999 C F FINNOX = GENNOX/2.205*BTUTOT/WTNOX F WRITE(NHSTRY,*)'FINNOX= ',FINNOX C SET THE EXPECTED CO GENERATION RATE, GENCO (LB/MMBTU) C F GENCO = 0.20 C THIS VALUE WAS OBTAINED FROM THE FWEC QUOTE IN THE REI FINAL C REPORT 1999 C F FINCO = GENCO/2.205*BTUTOT/WTCO C F WRITE(NHSTRY,*)'FINCO = ',FINCO F WRITE(NHSTRY,*)'WTCO =',WTCO EXECUTE BEFORE BLOCK M803CMB ; FORTRAN RADUACC F COMMON / HEATIN / BTUTOT DEFINE QTOT INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QM803T DEFINE HTLOSS BLOCK-VAR BLOCK=QCOMSPLT SENTENCE=FRAC & VARIABLE=FRAC ID1=QCOMLOSS C F UNACC = 0.003 F RADI = 0.003 F XMM = 0.01 C UNACC ARE THE UNACCOUNTED LOSSES C RADI ARE THE RADIANT LOSSES C XMM IS THE MANUFACTURER'S MARGIN C ALL ARE %S OF TOTAL HEAT TO THE BOILER C AND ARE BASED ON THE FWEC QUOTE 10/26/98 C F TLOSS = (UNACC + RADI + XMM)*(BTUTOT*1E6) C C CALCULATE THE HEAT FROM THE BOILER BEFORE THESE LOSSES C IN BTU/HR C F QOUT = QTOT*3600.*3.968E-3 C 3600 S/H AND 3.968E-3 BTU/CAL C F HTLOSS = TLOSS/QOUT C F WRITE(NHSTRY,*)'HTLOSS= ',HTLOSS READ-VARS QTOT WRITE-VARS HTLOSS ; FORTRAN PLNTELEC DEFINE WTOT INFO-VAR STRM=WTOTAL INFO=WORK VAR=POWER DEFINE WTOT2 INFO-VAR STRM=WTOTAL2 INFO=WORK VAR=POWER F WTOT2 = -WTOT EXECUTE AFTER M811GEN ; ;------------------------------------------------------------- ; STEAM CYCLE FORTRAN BLOCKS - AREA 8100 ;------------------------------------------------------------ ; FORTRAN XPSTMD ;THIS BLOCK CALCULATES THE TOTAL XHP STEAM DEMAND. ; DEFINE STMXP BLOCK-VAR BLOCK=M811XSPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=812D C REB IS THE STEAM REQUIRED FOR PRETREATMENT ; F STMXP = 0.0000001 ; WRITE-VARS STMXP ; FORTRAN HPSTMD ;THIS BLOCK CALCULATES THE TOTAL HP STEAM DEMAND. ; DEFINE STMHP BLOCK-VAR BLOCK=M811HSPT SENTENCE=MASS-FLOW & VARIABLE=FLOW ID1=814 DEFINE REB STREAM-VAR STREAM=216 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE F853 STREAM-VAR STREAM=853 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW C REB IS THE STEAM REQUIRED FOR PRETREATMENT ; F STMHP = REB + F853 ; READ-VARS REB F853 WRITE-VARS STMHP ; EXECUTE BEFORE M811HSPT ; FORTRAN LPSTMD c F COMMON /RXSPEC/ TEMPIN, CONCIN, TIME c THIS BLOCK CALCULATES THE TOTAL LP STEAM DEMAND. DEFINE STMDEM BLOCK-VAR BLOCK=M811ISPT SENT=MASS-FLOW & VARIABLE=FLOW ID1=815 DEFINE SACCHT STREAM-VAR STREAM=590 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE PTSTM STREAM-VAR STREAM=215 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SVSTM STREAM-VAR STREAM=596 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE TRIMST STREAM-VAR STREAM=592 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE REB STREAM-VAR STREAM=594 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; F STMDEM = SACCHT + PTSTM + SVSTM + TRIMST + REB f write(nhstry,20)saccht, ptstm, svstm, trimst, stmdem, reb f 20 format(' lp results',/, f 1 ' saccht= ',g12.5,/, f 2 ' ptstm= ',g12.5,/, f 3 ' svstm= 'g12.5,/, f 4 ' trimst= 'g12.5,/, f 5 ' stmdem= 'g12.5,/, f 6 ' reb = ',g12.5) READ-VARS SACCHT PTSTM SVSTM TRIMST REB WRITE-VARS STMDEM ; FORTRAN SETMAKUP ;THIS BLOCK CALCULATES THE LOSSES IN THE STEAM CYCLE DUE TO ;DIRECT STEAM INJECTION AND BOILER BLOWDOWN. STEAM DEMANDS ;TO HEAT EXCHANGERS ARE NOT INCLUDED BECAUSE THESE FLOWS ;SHOULD RETURN. ; DEFINE FMAKUP STREAM-VAR STREAM=811 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW DEFINE FBLOW STREAM-VAR STREAM=821 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW DEFINE FHPSTM STREAM-VAR STREAM=216 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW DEFINE FLPSTM STREAM-VAR STREAM=215 SUBSTREAM=MIXED & VARIABLE=MOLE-FLOW F FMAKUP = FHPSTM + FLPSTM + FBLOW EXECUTE BEFORE BLOCK T824AS ; ;-------------------------------------------------------- ; UTILITY FORTRAN BLOCKS - AREA 900 ;------------------------------------------------------- ; FORTRAN POW101 ; Calculates Power requirements for equipment in Area 100 from Harris ; Subcontract Information ; Power requirements are ratioed from 101's flow-rate DEFINE STV1 STREAM-VAR STREAM=101 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE STC1 STREAM-VAR STREAM=101 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW F TOTFLO1 = STV1 + STC1 ; Harris stated that power requirements are 75% of connected power ; and reported connected power for equipment so PWRRAT=0.75 ; Subcontract ACO-9-29067-01 ; Report 99-10600/13 page 4 F PWRRAT=0.75 ; Harris stated that 2500 gpm per line is the necessary water flow and ; designed the pumps for 5000 gpm so I set PMPREQ to 0.5 F PMPREQ=0.5 ; Harris' design was for 2000 bone dry metric tonnes / day at 15% moisture ; That is equivalent to 2594 short tons as recieved material / day ; Also equivalent to 98039 kg as received material / hr ; Subcontract ACO-9-29067-01 ; Report 99-10600/13 page 2 F FLORAT = 98039. ; Bale Transport Conveyors (C-101) ; 2 motors at 50 hp each = 100 hp = 74.57 kW for standard size facility ; (159948 kg/hr in 101) F PC101 = 74.57 DEFINE WWC101 INFO-VAR STREAM=WC101 INFO=WORK VARIABLE=POWER F WWC101 = PC101 * PWRRAT * TOTFLO1/FLORAT ; ; Bale Unwrapping Conveyors (C-102) ; 2 motors at 10 hp each = 20 hp = 14.91 kW for standard size facility ; (159948 kg/hr in 101) F PC102 = 14.91 DEFINE WWC102 INFO-VAR STREAM=WC102 INFO=WORK VARIABLE=POWER F WWC102 = PC102 * PWRRAT * TOTFLO1/FLORAT ; ; Shredder Feed Conveyor (C-104) ; 4 motors at 5 hp each = 20 hp = 14.91 kW for standard size facility ; (159948 kg/hr in 101) F PC104 = 14.91 DEFINE WWC104 INFO-VAR STREAM=WC104 INFO=WORK VARIABLE=POWER F WWC104 = PC104 * PWRRAT * TOTFLO1/FLORAT ; ; Belt Press Discharge Conveyor (C-105) ; 1 motors at 5 hp each = 5 hp = 3.73 kW for standard size facility ; (159948 kg/hr in 101) F PC103 = 3.73 DEFINE WWC103 INFO-VAR STREAM=WC103 INFO=WORK VARIABLE=POWER F WWC103 = PC103 * PWRRAT * TOTFLO1/FLORAT ; ; Wash Tables (M-104) ; 2 motors at 75 hp each = 150 hp = 111.86 kW for standard size facility ; (159948 kg/hr in 101) F PM104 = 111.86 DEFINE WWM104 INFO-VAR STREAM=WM104 INFO=WORK VARIABLE=POWER F WWM104 = PM104 * PWRRAT * TOTFLO1/FLORAT ; ; Wash Tables (M-105) ; 4 motors at 500 hp each = 2000 hp = 1491.4 kW for standard size facility ; (159948 kg/hr in 101) F PM105 = 1491.4 DEFINE WWM105 INFO-VAR STREAM=WM105 INFO=WORK VARIABLE=POWER F WWM105 = PM105 * PWRRAT * TOTFLO1/FLORAT ; ; Polymer Feed System (M-107) ; Minimal Power required so 25 kW for standard size facility ; (159948 kg/hr in 101) F PM107 = 25.0 / PWRRAT DEFINE WWM107 INFO-VAR STREAM=WM107 INFO=WORK VARIABLE=POWER F WWM107 = PM107 * PWRRAT * TOTFLO1/FLORAT ; ; Wash Table Pump (P-101) ; The listed pump design is 2500 gpm (0.1578 m^3/s) at 50 ft (21.68 psi) (App. A, p3) DEFINE WWP101 INFO-VAR STRM=WP101 INFO=WORK VAR=POWER ;C EPM is the pump efficiencies (set at 67% to get 100hp design like report) ;C EEL is the motor efficiencies F EPM = 0.67 F EEL = 0.95 F DP101 = 21.68 F AP101 = 0.1578 * PMPREQ c Two Units F EP101 = 2.0 F WWP101 = EP101 * (AP101 * (DP101*6894.8) / (EPM*EEL) ) / 1000. ; ; Wash Water Pump (P-102) ; The listed pump design is 5000 gpm (0.3155 m^3/s) at 50 ft (21.68 psi) (App. A, p5) DEFINE WWP102 INFO-VAR STRM=WP102 INFO=WORK VAR=POWER ;C EPM is the pump efficiencies (set at 67% to get 100hp design like report) ;C EEL is the motor efficiencies F DP102 = 21.68 F AP102 = 0.3155 * PMPREQ c Two Units F EP102 = 2.0 F WWP102 = EP102 * (AP102 * (DP102*6894.8) / (EPM*EEL) ) / 1000. ; ; Clarifier Underflow Feed Pump (P-103) ; The listed pump design is 100 gpm (0.00631 m^3/s) at 50 ft (21.68 psi) (App. A, p5) DEFINE WWP103 INFO-VAR STRM=WP103 INFO=WORK VAR=POWER ; EPM103 is the pump efficiencies (set at 16.9% to get 7.5hp design like report) ; EEL is the motor efficiencies F EPM103 = 0.169 F DP103 = 21.68 F AP103 = 0.00631 * PMPREQ c One Unit F EP103 = 1.0 F WWP103 = EP103 * (AP103 * (DP103*6894.8) / (EPM103*EEL) ) / 1000. ; ; Clarified Water Pump (P-104) ; The listed pump design is 5000 gpm (0.3155 m^3/s) at 50 ft (21.68 psi) (App. A, p5) DEFINE WWP104 INFO-VAR STRM=WP104 INFO=WORK VAR=POWER ;C EPM is the pump efficiencies (set at 67% to get 100hp design like report) ;C EEL is the motor efficiencies F DP104 = 21.68 F AP104 = 0.3155 * PMPREQ c One Unit F EP104 = 1.0 F WWP104 = EP104 * (AP104 * (DP104*6894.8) / (EPM*EEL) ) / 1000. ; ; Belt Press Sump Pump (P-105) ; The listed pump design is 100 gpm (0.00631 m^3/s) at 40 ft (17.34 psi) (App. A, p6) DEFINE WWP105 INFO-VAR STRM=WP105 INFO=WORK VAR=POWER C EPM105 is the pump efficiencies (set at 33.7% to get 3 hp design like report) F EPM105=0.337 C EEL is the motor efficiencies F DP105 = 17.34 F AP105 = 0.00631 * PMPREQ c One Unit F EP105 = 1.0 F WWP105 = EP105 * (AP105 * (DP105*6894.8) / (EPM105*EEL) ) / 1000. ; ; Clarifier Thickener (S-101) ; 1 motors at 10 hp each = 10 hp = 7.457 kW for standard size facility ; (159948 kg/hr in 101) F PS101 = 7.457 DEFINE WWS101 INFO-VAR STREAM=WS101 INFO=WORK VARIABLE=POWER F WWS101 = PS101 * PWRRAT * TOTFLO1/FLORAT ; ; Belt Filter (S-102) ; 1 units at 7.5 hp each = 7.5 hp = 5.59 kW for standard size facility ; (159948 kg/hr in 101) F PS102 = 5.59 DEFINE WWS102 INFO-VAR STREAM=WS102 INFO=WORK VARIABLE=POWER F WWS102 = PS102 * PWRRAT * TOTFLO1/FLORAT READ-VARS STV1 STC1 WRITE-VARS WWC101 WWC102 WWC104 WWC103 & WWM104 WWM105 WWM107 & WWP101 WWP102 WWP103 WWP104 WWP105 & WWS101 WWS102 ; FORTRAN POWER DEFINE CLVES PARAMETER 43 DEFINE CLVOL PARAMETER 44 ; ;THIS BLOCK CALCULATES THE AGITATION REQUIREMENT FOR MIXERS ; AND FERMENTORS. THE FOLLOWING SYMBOLISM IS USED IN THIS ;BLOCK. c c POWER REQUIREMENTS FOR EACH STREAM ARE IN KW/L (**P) c ; Unless Otherwise Stated c THESE POWER REQUIREMENTS WAS OBTAINED FROM THE c 1990 BASE CASE. EXCEPTIONS INCLUDE THOSE FOR c WASTEWATER TREATMENT WHICH WERE OBTAINED FROM c THE 1995 CHEM SYSTEMS STUDY AND THE CH2MHILL c REPORT. They are listed in kW/L. 3.94E-4 kW/L=2 hp/1000 gal. c c c THE RESIDENCE TIME FOR EACH VESSEL IS IN HOURS (**R) c c THE RESIDENCE TIMES (h) WERE TAKEN FROM THE 1990 BASE c CASE EXCEPT FOR THOSE FOR WASTEWATER TREATMENT c WHICH WERE TAKEN FROM THE 1995 CHEM SYSTEMS STUDY AND c FROM THE CH2MHILL REPORT. c c c THE POWER FOR EACH VESSEL IS CALCULATED IN KW (**MXP) c ;OL - OVERLIMING TANK AGITATOR (A-209) DEFINE OL STREAM-VAR STREAM=228 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE OLD STREAM-VAR STREAM=228 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE OLS STREAM-VAR STREAM=228 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE OLDS STREAM-VAR STREAM=228 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE OLMXP INFO-VAR STREAM=WT209 INFO=WORK & VARIABLE=POWER F OLV=OL/OLD+OLS/OLDS c 9.85E-5 kW/L=0.5 hp/1000 gal F OLP=9.85E-5 c 1 hr. residence time from Delta T F OLR=1 F OLMXP=OLV*OLR*OLP ;XNT - REACIDIFICATION TANK AGITATOR (A-224) DEFINE XNT STREAM-VAR STREAM=239 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE XNTD STREAM-VAR STREAM=239 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE XNTS STREAM-VAR STREAM=239 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE XNTDS STREAM-VAR STREAM=239 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE XNTMXP INFO-VAR STREAM=WT224 INFO=WORK & VARIABLE=POWER F XNTV=XNT/XNTD+XNTS/XNTDS ; 0.5 hp/1000 gal = 9.85E-5 kW/L F XNTP=9.85E-5 ; Residence Time 4 hours F XNTR=4 F XNTMXP=XNTV*XNTR*XNTP ;HMT - HYDROLYSATE MIX TANK AGITATOR (A-205) DEFINE HMT STREAM-VAR STREAM=220 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE HMTD STREAM-VAR STREAM=220 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE HMTS STREAM-VAR STREAM=220 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE HMTDS STREAM-VAR STREAM=220 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE HMTMXP INFO-VAR STREAM=WT205 INFO=WORK & VARIABLE=POWER F HMTV=HMT/HMTD+HMTS/HMTDS ; 2.96E-4 kW/L=1.5 hp/1000 gal F HMTP=2.96E-4 F HMTR=0.25 F HMTMXP=HMTV*HMTR*HMTP ;SLT - SLURRYING TANK AGITATOR (A-232) DEFINE SLT STREAM-VAR STREAM=250 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SLTD STREAM-VAR STREAM=250 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE SLTS STREAM-VAR STREAM=250 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE SLTDS STREAM-VAR STREAM=250 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE SLTMXP INFO-VAR STREAM=WT232 INFO=WORK & VARIABLE=POWER F SLTV=SLT/SLTD+SLTS/SLTDS ; 2.96E-4 kW/L=1.5 hp/1000 gal F SLTP=2.96E-4 F SLTR=0.25 F SLTMXP=SLTV*SLTR*SLTP ; ; ;SD - ZYMOMONAS SEED FERMENTOR AGITATORS (A-303-305A/B&306A-F) DEFINE SD STREAM-VAR STREAM=306 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE SDD STREAM-VAR STREAM=306 SUBSTREAM=MIXED VARIABLE=MASS-DENSITY DEFINE SDS STREAM-VAR STREAM=306 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW DEFINE SDSD STREAM-VAR STREAM=306 SUBSTREAM=CISOLID VARIABLE=MASS-DENSITY DEFINE SDMXP INFO-VAR STREAM=WT305 INFO=WORK VARIABLE=POWER DEFINE SDMXP2 INFO-VAR STREAM=WT304 INFO=WORK VARIABLE=POWER ; Calculate the volumetric flow to F-305 (stream 306) F SDV = (SD/SDD + SDS/SDSD) ; Calculate the volume as 10% (inoculum level) F SDV = SDV * 0.1 ; 0.1 HP/1000 GAL = 1.97e-5 KW/L F SDP = 1.97E-5 ; One batch turns around each 24 hrs. So this is the effective residence time F SDR = 24. ; SDNU is the number of Zymo Seed trains on line at any one time F SDNU = 2. ; Calculate Power F SDMXP = SDNU * SDV * SDR * SDP c Then A-304 c SDN2 is the volume ratio of F-304 to F-305 F SDN2 = 0.1 c SDP2 is the mixing power for A-304 (5.91E-5=0.3 hp/1000 gal) F SDP2 = 5.91E-5 ; Calculate Power F SDMXP2 = SDP2 * (SDNU * SDV * SDR) * SDN2 ; ;ZM - ZYMOMONAS HOLD TANK AGITATORS (A-301) DEFINE ZMMXP INFO-VAR STREAM=WT301 INFO=WORK VARIABLE=POWER ; ; ZMINC=VOLUME RATIO OF SEED HOLD TO LARGEST SEED TANK ; F ZMINC=1.2 ; ; 0.1 HP/1000 GAL = 1.97E-5 KW/L ; F ZMP=1.97E-5 ; ; 24 hr Residence time, Same as F-305 (Largest Seed) ; F ZMR=24 ; ; SDV (calculated earlier), volumetric flow to F-305 ; SDV*ZMR = volume of F-305 ; F ZMMXP=(SDV*ZMR) * ZMINC * ZMP ; ;SA - SACCHARIFICATION TANK AGITATORS (A-310) ; Use hp requirements of SSCF fermentors; the requirements may be higher ; and the ferms lower when separate sacch. and fermentation DEFINE SA STREAM-VAR STREAM=301B SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE SAD STREAM-VAR STREAM=301B SUBSTREAM=MIXED VARIABLE=MASS-DENSITY DEFINE SAS STREAM-VAR STREAM=301B SUBSTREAM=CISOLID VARIABLE=MASS-FLOW DEFINE SASD STREAM-VAR STREAM=301B SUBSTREAM=CISOLID VARIABLE=MASS-DENSITY DEFINE SAMXP INFO-VAR STREAM=WT310 INFO=WORK VARIABLE=POWER DEFINE SACVES PARAMETER 36 DEFINE SACDAY PARAMETER 37 DEFINE SACVOL PARAMETER 38 DEFINE SACWV PARAMETER 39 ; Calculate Volumetric Flow Rate F SAV = SA/SAD + SAS/SASD ; 0.15 HP/1000 GAL = 2.9549e-5 KW/L F SAP = 2.9549E-5 ; SACDAY is the Sacch. residence time in days. F SAR = SACDAY * 24 F SAMXP = SAV * SAR * SAP ; Calculate the number of Sacch. tanks required for costing F SACVES = SAV * SAR / SACVOL / SACWV ; ;SM - FERMENTOR AGITATORS (A-300) DEFINE SM STREAM-VAR STREAM=306 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE SMD STREAM-VAR STREAM=306 SUBSTREAM=MIXED VARIABLE=MASS-DENSITY DEFINE SMS STREAM-VAR STREAM=306 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW DEFINE SMSD STREAM-VAR STREAM=306 SUBSTREAM=CISOLID VARIABLE=MASS-DENSITY DEFINE SMMXP INFO-VAR STREAM=WT300 INFO=WORK VARIABLE=POWER DEFINE SSFVES PARAMETER 31 DEFINE SSFDAY PARAMETER 32 DEFINE SSFVOL PARAMETER 33 DEFINE SSFWV PARAMETER 34 ; Calculate Volumetric Flow Rate F SMV = SM/SMD + SMS/SMSD ; 0.15 HP/1000 GAL = 2.9549e-5 KW/L F SMP = 2.9549E-5 ; SSFDAY is the SSCF residence time in days. F SMR = SSFDAY * 24 F SMMXP = SMV * SMR * SMP ; Calculate the number of SSCF vessels required for costing F SSFVES = SMV * SMR / SSFVOL / SSFWV ; ;BW - BEER WELL DEFINE BW STREAM-VAR STREAM=502 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE BWD STREAM-VAR STREAM=502 SUBSTREAM=MIXED VARIABLE=MASS-DENSITY DEFINE BWS STREAM-VAR STREAM=502 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW DEFINE BWSD STREAM-VAR STREAM=502 SUBSTREAM=CISOLID VARIABLE=MASS-DENSITY DEFINE BWMXP INFO-VAR STREAM=WT306 INFO=WORK VARIABLE=POWER ; Calculate Volumetric Flow F BWV = BW/BWD + BWS/BWSD ; 0.3 HP/1000 GAL = 5.91e-5 KW/L F BWP = 5.91E-5 ; BWR is the Beer Well Residence time in hrs F BWR = 4 F BWMXP = BWV * BWR * BWP ; ;CS - CELLULASE SEED FERMENTOR AGITATORS (A-402-3A/B) DEFINE CSD STREAM-VAR STREAM=433 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CSDD STREAM-VAR STREAM=433 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE CSDS STREAM-VAR STREAM=433 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE CSDSD STREAM-VAR STREAM=433 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE CSMXP INFO-VAR STREAM=WT402-3 INFO=WORK & VARIABLE=POWER c First calculate for A-403 F CSV=CSD/CSDD+CSDS/CSDSD ; 10.2 HP/1000 GAL = 1.972E-3 F CSP=1.972E-3 F CSR=24 ; CSNU is the number of cellulase seed trains use F CSNU=3 F CSMXP=CSNU*CSV*CSR*CSP c Then for A-402 c CSR3 is the volume ratio of F-402 to F-403 F CSR3=0.05 c CSP3 is the power requirement for A-402 (5.20E-3 kW/L=26.4hp/1000 gal) F CSP3=5.2E-3 F CSMXP=CSMXP + CSNU*CSV*CSR*CSR3*CSP3 ;CL - CELLULASE FERMENTOR AGITATORS (A-400A-L) c CLV is the volume (in liters) of the cellulase production ferms c it is calculated from variables calculated in AIRREQ DEFINE CLMXP INFO-VAR STREAM=WT400 INFO=WORK & VARIABLE=POWER F CLV=(CLVES-3)*CLVOL c 4.48E-4 kW/L= 2.2727 hp/1000 gal = 600 hp / 264000 gal c (from Lightnin Quote -- on full volume basis) F CLP=4.48E-4 F CLMXP=CLV*CLP ;PM - MEDIA PREP TANK AGITATOR (T-405) DEFINE PM STREAM-VAR STREAM=416 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE PMD STREAM-VAR STREAM=416 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE PMS STREAM-VAR STREAM=416 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE PMSD STREAM-VAR STREAM=416 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE PMMXP INFO-VAR STREAM=WT405 INFO=WORK & VARIABLE=POWER F PMV=PM/PMD+PMS/PMSD c 0.2 hp/1000 gal = 39.40E-6 kW/L F PMP=39.4E-6 C Residence Time 36 hr F PMR=36 F PMMXP=PMV*PMP*PMR F WRITE(NHSTRY,*)'PMV=',PMV,'PMR=',PMR,'PMMXP=',PMMXP ;EQ - EQUALIZATION BASIN AGITATOR (A-602) DEFINE AB STREAM-VAR STREAM=612 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE ABD STREAM-VAR STREAM=612 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE ABS STREAM-VAR STREAM=612 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE ABSD STREAM-VAR STREAM=612 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE EQMXP INFO-VAR STREAM=WT602 INFO=WORK & VARIABLE=POWER F EQV=AB/ABD c 0.1 hp/1000 gal = 19.70E-6 kW/L F EQP=19.7E-6 C Residence Time 7.2 hr F EQR=7.2 F EQMXP=EQV*EQP*EQR F WRITE(NHSTRY,*)'EQV=',EQV,'EQR=',EQR,'EQMXP=',EQMXP ;RW - RECYCLE WATER TANK AGITATOR (A-530) DEFINE RW2 STREAM-VAR STREAM=572 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE RWD2 STREAM-VAR STREAM=572 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE RWS2 STREAM-VAR STREAM=572 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE RWSD2 STREAM-VAR STREAM=572 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE RWMXP INFO-VAR STREAM=WT530 INFO=WORK & VARIABLE=POWER F RWV=RW2/RWD2+RWS2/RWSD2 C Power from vendor quote 0.4 hp/1000 gal, 78.8 kW/L F RWP=78.8E-6 C Residence time 20 minutes, 0.333 hours F RWR=0.3333 F RWMXP=RWV*RWP*RWR ;CSL - CSL STORAGE TANK AGITATOR (A-720) DEFINE CSLT STREAM-VAR STREAM=735 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE CSLTD STREAM-VAR STREAM=735 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE CSLTS STREAM-VAR STREAM=735 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE CSLTDS STREAM-VAR STREAM=735 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE CSLMXP INFO-VAR STREAM=WT720 INFO=WORK & VARIABLE=POWER F CSLTV=CSLT/CSLTD+CSLTS/CSLTDS ; 0.1 hp/1000 gal = 1.97E-5 kW/L (based on A-301) F CSLTP=1.97E-5 ; Residence Time 120 hours (guess by AA 02/22/01) ; (because T720 has a 120 hr residence time) F CSLTR=120 F CSLMXP=CSLTV*CSLTR*CSLTP ; ;DAP - CSL/DAP DAY TANK AGITATOR (A-760) DEFINE DAPT STREAM-VAR STREAM=735 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE DAPTD STREAM-VAR STREAM=735 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE DAPTS STREAM-VAR STREAM=735 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE DAPTDS STREAM-VAR STREAM=735 SUBSTREAM=CISOLID & VARIABLE=MASS-DENSITY DEFINE DAPMXP INFO-VAR STREAM=WT760 INFO=WORK & VARIABLE=POWER F DAPTV=DAPT/DAPTD+DAPTS/DAPTDS ; 0.5 hp/1000 gal = 9.85E-5 kW/L (based on ?) F DAPTP=9.85E-5 ; Residence Time is about 28 hours ; CSL flow rate is 372 gph (1300 kg/hr) and T-760 is 10,000 gal ; =>10,000/372 = 28 hours F DAPTR=28 F DAPMXP=DAPTV*DAPTR*DAPTP ; ; f WRITE(NHSTRY,'('' **** WKMIX RESULTS ****'')') F WRITE(NHSTRY,'('' SMMXP '',G12.5)')SMMXP F WRITE(NHSTRY,'('' SDMXP '',G12.5)')SDMXP F WRITE(NHSTRY,'('' SMV '',G12.5)')SMV F WRITE(NHSTRY,'('' SDV '',G12.5)')SDV F WRITE(NHSTRY,'('' SM '',G12.5)')SM F WRITE(NHSTRY,'('' SMD '',G12.5)')SMD F WRITE(NHSTRY,'('' SD '',G12.5)')SD F WRITE(NHSTRY,'('' SDD '',G12.5)')SDD READ-VARS OL OLD OLS OLDS XNT XNTD XNTS XNTDS & HMT HMTD HMTS HMTDS & SLT SLTD SLTS SLTDS SD SDD SDS SDSD & SA SAD SAS SASD & SM SMD SMS SMSD CSD CSDD CSDS CSDSD & AB ABD ABS ABSD & PM PMD PMS PMSD & RW2 RWD2 RWS2 RWSD2 & CSLT CSLTD CSLTS CSLTDS & DAPT DAPTD DAPTS DAPTDS & SSFDAY SSFVOL SSFWV CLVES CLVOL WRITE-VARS SSFVES SACVES OLMXP XNTMXP HMTMXP & SLTMXP SDMXP ZMMXP & SAMXP SMMXP CSMXP CLMXP EQMXP PMMXP & RWMXP CSLMXP DAPMXP ; EXECUTE BEFORE PUMPS ; ; FORTRAN PUMPS ; Calculates the electrical work required by each pump not specifically ; simulated. ; C Each differential presure (DP) term is the pump head and is in psi C In the WP equations DP is converted to N/m^2 C C Flows (FMs & FCs) are Retrieved in Kg/hr & converted to Kg/s C Densities (RMs & RCs) are retrieved in Kg/L & converted to Kg/m^3 C Power is calculated in kW (N m/s, J/s) C C Convert psi * 6894.8 = N/m^2 C Convert Kg/hr * 1/3600 = Kg/s C Convert Kg/L * 1000 = Kg/m^3 C Convert W /1000 = kW ; P-201 Sulfuric Acid Pump DEFINE FMP201 STREAM-VAR STRM=710 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP201 STREAM-VAR STRM=710 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP201 STREAM-VAR STRM=710 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP201 STREAM-VAR STRM=710 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP201 INFO-VAR STRM=WP201 INFO=WORK VAR=POWER C EPM is the pump efficiencies C EEL is the motor efficiencies F EPM = 0.60 F EEL = 0.95 c 250 ft. head of sulfuric acid (dens. 1.8)= 191.1 psi F DP201 =191.1 F AP201 =(FMP201/3600.)/(RMP201*1000.)+(FCP201/3600.)/(RCP201*1000.) F WP201 =(AP201 * (DP201*6894.8) / (EPM*EEL) ) / 1000. ; P-205 Pneumapress Feed Pumps DEFINE STC220 STREAM-VAR STREAM=220 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW C Power based on the solids flow of stream 220 C DEFINE WP205 INFO-VAR STREAM=WP205 INFO=WORK VARIABLE=POWER ; ; Power Required from Harris design (300 hp at 75% power) ; equals 225 hp / Flow from R0101C (see equip design ; sheet) ; Power Required 225 hp / 50299 kg/hr CISOLIDS flow = 4.47E-3 hp/kg/hr ; = 3.33E-3 kW/kg/hr F HF = 3.33E-3 F WP205 = HF * STC220 ; ; P-209 Overlimed Hydrolysate Pump DEFINE FMP209 STREAM-VAR STRM=228 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP209 STREAM-VAR STRM=228 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP209 STREAM-VAR STRM=228 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP209 STREAM-VAR STRM=228 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE AWP209 INFO-VAR STRM=WP209 INFO=WORK VAR=POWER c 150 ft. head = 65 psi F DP209 = 65.0 F AP209 =(FMP209/3600.)/(RMP209*1000.)+(FCP209/3600.)/(RCP209*1000.) F AWP209 =(AP209 * (DP209*6894.8) / (EPM*EEL) ) / 1000. ; P-222 Overlimed Hydrolysate Liquor Pump DEFINE FMP222 STREAM-VAR STRM=230 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP222 STREAM-VAR STRM=230 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP222 STREAM-VAR STRM=230 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP222 STREAM-VAR STRM=230 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP222 INFO-VAR STRM=WP222 INFO=WORK VAR=POWER c 150 ft. head = 65 psi F DP222 = 65.0 F AP222 =(FMP222/3600.)/(RMP222*1000.)+(FCP222/3600.)/(RCP222*1000.) F WP222 =(AP222 * (DP222*6894.8) / (EPM*EEL) ) / 1000. ; P-211 Concentrated Filtrate Pumps DEFINE FMP211 STREAM-VAR STRM=221 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE FCP211 STREAM-VAR STRM=221 SUBSTREAM=CISOLID VAR=MASS-FLOW C Power based on the total flow of 221 C DEFINE WP211 INFO-VAR STREAM=WP211 INFO=WORK VARIABLE=POWER ; ; Power Required from Harris design (25 hp at 75% power) ; equals 18.8 hp / Flow from R0101C (see equip design ; sheet) ; Power Required 18.8 hp / 136350 kg/hr CISOLIDS flow = 1.38E-4 hp/kg/hr ; = 1.03E-4 kW/kg/hr F HP211 = 1.03E-4 F WP211 = HP211 * (FMP211 + FCP211) ; ; P-213 Wash Filtrate Pump #2 DEFINE F256 STREAM-PROP STREAM=256 PROPERTY=MASSFLW C Power based on the total flow of 256 C DEFINE WP213 INFO-VAR STREAM=WP213 INFO=WORK VARIABLE=POWER ; ; Power Required from Harris design (400 hp at 75% power) ; equals 300.0 hp / Flow from R0101C (see equip design ; sheet) ; Power Required 300.0 hp / 131530 kg/hr CISOLIDS flow = 2.28E-3 hp/kg/hr ; = 1.70E-3 kW/kg/hr F HP213 = 1.70E-3 F WP213 = HP213 * F256 ; ; P-224 Fermentation Feed Pump DEFINE FMP224 STREAM-VAR STRM=232 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP224 STREAM-VAR STRM=232 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP224 STREAM-VAR STRM=232 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP224 STREAM-VAR STRM=232 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP224 INFO-VAR STRM=WP224 INFO=WORK VAR=POWER c P-224 is a rotary lobe pump, so the power req. is not calculated c like a centrifugal pump. It has an input of 1.231E-2 kW/ L/min c (50 hp/800 gpm) F PP224=1.231E-2 F AP224 =(FMP224/60.)/(RMP224)+(FCP224/60.)/(RCP224) F WP224 =AP224 * PP224 ; P-239 Reacidified Liquor Pump DEFINE FMP239 STREAM-VAR STRM=239 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP239 STREAM-VAR STRM=239 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP239 STREAM-VAR STRM=239 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP239 STREAM-VAR STRM=239 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP239 INFO-VAR STRM=WP239 INFO=WORK VAR=POWER c 100 ft head = 43.4 F DP239 = 43.4 F AP239 =(FMP239/3600.)/(RMP239*1000.)+(FCP239/3600.)/(RCP239*1000.) F WP239 =(AP239 * (DP239*6894.8) / (EPM*EEL) ) / 1000. ; P-310 Saccharified Slurry Transfer Pump ; Using same parameters as fermentation (SSF) transfer pump DEFINE FMP310 STREAM-VAR STRM=301B SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP310 STREAM-VAR STRM=301B SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP310 STREAM-VAR STRM=301B SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP310 STREAM-VAR STRM=301B SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP310 INFO-VAR STRM=WP310 INFO=WORK VAR=POWER DEFINE QSAC INFO-VAR STREAM=QF300A INFO=HEAT VARIABLE=DUTY DEFINE SACVES PARAMETER 36 DEFINE PMPSAC PARAMETER 40 ; ; Calculate the pump-around flow to cool Saccharified Slurry ; DELTAT=temperature decrease of slurry in heat exchanger ; CPMIX=heat capacity of mixed stream (cal / g C) ; CPCI=heat capacity of CI solid stream (cal /g C) ; FRCMIX =mixed fraction of stream 301B ; FRCCI = CI solids fraction of stream 301B ; PMPSAC = Pumparound flow rate for Saccharification (same as SSCF) ; SACVES = Number of Sacch. tanks from common block ; RECFKW = Individual Pump Recirculation Flow ; FRDFLW = Individual pump forward flow ; F DELTAT = 2.0 F CPMIX = 1.0 F CPCI = 1.0 F FRCMIX = FMP310/(FMP310+FCP310) F FRCCI = 1-FRCMIX c PMPSAC is first calculated in g/sec F PMPSAC = QSAC / (DELTAT * (FRCMIX * CPMIX + FRCCI * CPCI)) F WRITE(NHSTRY,*)' PMPSAC1: ',PMPSAC ; Three parallel trains (approximately) ; Calculate the forward flow through each train F FRWFLW = (FMP310 + FCP310) / 3. ; Individual Pump Recirculation Flow (divided by total number of pumps) F RECFLW = (PMPSAC*3600/1000) / SACVES ; Total Pump Flow F PMPSAC = ( RECFLW + FRWFLW ) * SACVES ; 138.6 FT. HEAD = 60 PSI F DP310 = 60.0 F AP310 =(PMPSAC*FRCMIX/3600.)/(RMP310*1000.) F AP310 =AP310+(FCP310*(1-FRCMIX)/3600.)/(RCP310*1000.) F WP310 =(AP310 * (DP310*6894.8) / (EPM*EEL) ) / 1000. F WRITE(NHSTRY,*)' QSAC: ',QSAC F WRITE(NHSTRY,*)' SACVES: ',SACVES F WRITE(NHSTRY,*)' FMP310: ',FMP310 F WRITE(NHSTRY,*)' RMP310: ',RMP310 F WRITE(NHSTRY,*)' FCP310: ',FCP310 F WRITE(NHSTRY,*)' RCP310: ',RCP310 F WRITE(NHSTRY,*)' WP310: ',WP310 F WRITE(NHSTRY,*)' PMPSAC: ',PMPSAC F WRITE(NHSTRY,*)' FRWFLW: ',FRWFLW F WRITE(NHSTRY,*)' RECFLW: ',RECFLW ; P-300 SSCF Transfer Pump DEFINE FMP300 STREAM-VAR STRM=306 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP300 STREAM-VAR STRM=306 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP300 STREAM-VAR STRM=306 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP300 STREAM-VAR STRM=306 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP300 INFO-VAR STRM=WP300 INFO=WORK VAR=POWER DEFINE QREM INFO-VAR STREAM=QF300 INFO=HEAT VARIABLE=DUTY DEFINE SSFVES PARAMETER 31 DEFINE PMPSSF PARAMETER 35 ; ; Calculate the pump-around flow to cool SSCF broth ; DELTAT=temperature decrease of broth in heat exchanger ; CPMIX=heat capacity of mixed stream (cal / g C) ; CPCI=heat capacity of CI solid stream (cal /g C) ; FRCMIX =mixed fraction of stream 306 ; FRCCI = CI solids fraction of stream 306 ; PMPSSF = Pumparound flow rate for SSCF ; SSFVES = Number of SSF vessels from common block ; RECFKW = Individual Pump Recirculation Flow ; FRDFLW = Individual pump forward flow ; F DELTAT = 2.0 F CPMIX = 1.0 F CPCI = 1.0 F FRCMIX = FMP300/(FMP300+FCP300) F FRCCI = 1-FRCMIX c PMPSSF is first calculated in g/sec F PMPSSF = QREM / (DELTAT * (FRCMIX * CPMIX + FRCCI * CPCI)) F WRITE(NHSTRY,*)' PMPSSF1: ',PMPSSF ; Three parallel trains (approximately) ; Calculate the forward flow through each train F FRWFLW = (FMP300 + FCP300) / 3. ; Individual Pump Recirculation Flow (divided by total number of pumps) F RECFLW = (PMPSSF*3600/1000) / SSFVES ; Total Pump Flow F PMPSSF = ( RECFLW + FRWFLW ) * SSFVES ; 138.6 FT. HEAD = 60 PSI F DP300 = 60.0 F AP300 =(PMPSSF*FRCMIX/3600.)/(RMP300*1000.) F AP300 =AP300+(FCP300*(1-FRCMIX)/3600.)/(RCP300*1000.) F WP300 =(AP300 * (DP300*6894.8) / (EPM*EEL) ) / 1000. F WRITE(NHSTRY,*)' QREM: ',QREM F WRITE(NHSTRY,*)' SSFVES: ',SSFVES F WRITE(NHSTRY,*)' FMP300: ',FMP300 F WRITE(NHSTRY,*)' RMP300: ',RMP300 F WRITE(NHSTRY,*)' FCP300: ',FCP300 F WRITE(NHSTRY,*)' RCP300: ',RCP300 F WRITE(NHSTRY,*)' WP300: ',WP300 F WRITE(NHSTRY,*)' PMPSSF: ',PMPSSF F WRITE(NHSTRY,*)' FRWFLW: ',FRWFLW F WRITE(NHSTRY,*)' RECFLW: ',RECFLW ; P-301 SSCF Seed Transfer Pump DEFINE FMP301 STREAM-VAR STRM=304 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP301 STREAM-VAR STRM=304 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP301 STREAM-VAR STRM=304 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP301 STREAM-VAR STRM=304 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP301 INFO-VAR STRM=WP301 INFO=WORK VAR=POWER DEFINE WP302 INFO-VAR STRM=WP302 INFO=WORK VAR=POWER c P-301 & P-302 are rotary lobe pumps, so the power req. not calculated c like a centrifugal pump. It has an input of 2.462E-2 kW/ L/min c (100 hp/800 gpm) c P-302 is a larger pump, but doesn't run all of the time. On the c average it is the same as P-301 F PP301 = 2.462E-2 F AP301 = (FMP301/60.)/(RMP301)+(FCP301/60.)/(RCP301) F WP301 = AP301 * PP301 F WP302 = WP301 ; P-306 Beer Transfer Pump DEFINE FMP306 STREAM-VAR STRM=502 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP306 STREAM-VAR STRM=502 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP306 STREAM-VAR STRM=502 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP306 STREAM-VAR STRM=502 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP306 INFO-VAR STRM=WP306 INFO=WORK VAR=POWER ; 170 FT = 73.7 PSI F DP306 = 73.7 F AP306 =(FMP306/3600.)/(RMP306*1000.)+(FCP306/3600.)/(RCP306*1000.) F WP306 =(AP306 * (DP306*6894.8) / (EPM*EEL) ) / 1000. ; ; P-400 Cellulase Transfer Pump DEFINE FMP400 STREAM-VAR STRM=420 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP400 STREAM-VAR STRM=420 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP400 STREAM-VAR STRM=420 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP400 STREAM-VAR STRM=420 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP400 INFO-VAR STRM=WP400 INFO=WORK VAR=POWER ; 43.3 psi=100.0 ft head F DP400 = 43.3 F AP400 =(FMP400/3600.)/(RMP400*1000.)+(FCP400/3600.)/(RCP400*1000.) F WP400 =(AP400 * (DP400*6894.8) / (EPM*EEL) ) / 1000. ; P-401 Cellulase Seed Transfer Pump DEFINE FMP401 STREAM-VAR STRM=433 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP401 STREAM-VAR STRM=433 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP401 STREAM-VAR STRM=433 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP401 STREAM-VAR STRM=433 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP401 INFO-VAR STRM=WP401 INFO=WORK VAR=POWER c P-401 is a rotary lobe pump, so the power req. is not calculated c like a centrifugal pump. It has an input of 1.77E-2 kW/ L/min c (6.5 hp/72.5 gpm per Delta T) F PP401 = 1.77E-2 F AP401 =(FMP401/60.)/(RMP401)+(FCP401/60.)/(RCP401) F WP401 =AP401 * PP401 ; ; P-405 Media Pump DEFINE FMP405 STREAM-VAR STRM=416 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP405 STREAM-VAR STRM=416 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP405 STREAM-VAR STRM=416 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP405 STREAM-VAR STRM=416 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP405 INFO-VAR STRM=WP405 INFO=WORK VAR=POWER ; 44.3 psi=100 ft head F DP405 = 44.3 F AP405 =(FMP405/3600.)/(RMP405*1000.)+(FCP405/3600.)/(RCP405*1000.) F WP405 =(AP405 * (DP405*6894.8) / (EPM*EEL) ) / 1000. ; P-420 Antifoam Pump DEFINE FMP420 STREAM-VAR STRM=417 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP420 STREAM-VAR STRM=417 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP420 STREAM-VAR STRM=417 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP420 STREAM-VAR STRM=417 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP420 INFO-VAR STRM=WP420 INFO=WORK VAR=POWER c 33 psi = 75 ft. head F DP420 = 33 F AP420 =(FMP420/3600.)/(RMP420*1000.)+(FCP420/3600.)/(RCP420*1000.) F WP420 =(AP420 * (DP420*6894.8) / (EPM*EEL) ) / 1000. ; P-501 Beer Column Bottoms Pump DEFINE FMP501 STREAM-VAR STRM=518 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP501 STREAM-VAR STRM=518 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP501 STREAM-VAR STRM=518 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP501 STREAM-VAR STRM=518 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE QREB INFO-VAR STRM=QRD501 INFO=HEAT VARIABLE=DUTY DEFINE WP501 INFO-VAR STRM=WP501 INFO=WORK VAR=POWER DEFINE P501GP PARAMETER 5 C C Pump Flow = Recirc Flow + Bottoms Flow C Bottoms Flow = Stream 518 C Recirc Flow(gpm)=QRD501(BTU/hr)/1.21E8(BTU/hr)*3827 gpm(from Delta-T) C C Flow of 518 in M^3/S F AP501 =(FMP501/3600.)/(RMP501*1000.)+(FCP501/3600.)/(RCP501*1000.) C Flow of 518 in gpm F GP501 = AP501 * 15850.45 C QRD501 in BTU/hr F QBTU = -(QREB * 14.2869) C Recirc Flow in gpm F GPMREC = (QBTU / 1.21E8) * 3827. C Recirc Flow in m^3/s F APREC = GPMREC / 15850.45 F WRITE(NHSTRY,*)' AP501 = ',ap501,' GP501 = ',gp501,' QBTU = ',qbtu F WRITE(NHSTRY,*)' GPMREC = ',gpmrec,' APREC = ',aprec C Total Flow F AP501 = AP501 + APREC F P501GP = AP501 * 15850.45 c 67.5 psi=150 ft head F DP501 = 67.5 F WP501 =(AP501 * (DP501*6894.8) / (EPM*EEL) ) / 1000. F WRITE(NHSTRY,*)' AP501 = ',AP501,' WP501 = ',WP501 F WRITE(NHSTRY,*)' P501GP = ',P501GP ; P-503 Beer Column Reflux Pump ; DEFINE FP503B STREAM-VAR STRM=PS506 SUBSTREAM=CISOLID VAR=MASS-FLOW ; DEFINE RP503B STREAM-VAR STRM=PS506 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP503 INFO-VAR STRM=WP503 INFO=WORK VAR=POWER c 60.7 psi = 140 ft head F DP503 = 60.7 c Assume flow is 2500 kg/hr & density is 1kg/L F AP503 =(2500/3600.)/(1.*1000.) F WP503 =(AP503 * (DP503*6894.8) / (EPM*EEL) ) / 1000. ; P-504 Rectification Column Bottoms Pump DEFINE FMP504 STREAM-VAR STRM=516 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP504 STREAM-VAR STRM=516 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP504 STREAM-VAR STRM=516 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP504 STREAM-VAR STRM=516 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP504 INFO-VAR STRM=WP504 INFO=WORK VAR=POWER c 66 psi = 155 ft. head F DP504 = 66. F AP504 =(FMP504/3600.)/(RMP504*1000.)+(FCP504/3600.)/(RCP504*1000.) F WP504 =(AP504 * (DP504*6894.8) / (EPM*EEL) ) / 1000. F WRITE(NHSTRY,71)AP504,WP504 F 71 FORMAT('MISC RESULTS',/, F 1 'AP504=',G12.5,/, F 2 'WP504=',G12.5) ; P-505 Rectification Column Reflux Pump ; DEFINE FMP505 STREAM-VAR STRM=PS511 SUBSTREAM=MIXED VAR=MASS-FLOW ; DEFINE RMP505 STREAM-VAR STRM=PS511 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE WP505 INFO-VAR STRM=WP505 INFO=WORK VAR=POWER c 47.5 psi = 109.5 ft. head F DP505 = 47.5 c Assume flow is 80000 kg/hr and density is 1kg/L F AP505 =(80000/3600.)/(1*1000.) F WP505 =(AP505 * (DP505*6894.8) / (EPM*EEL) ) / 1000. ; P-511 1st Effect Pump DEFINE FMP511 STREAM-VAR STRM=525 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP511 STREAM-VAR STRM=525 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP511 STREAM-VAR STRM=525 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP511 STREAM-VAR STRM=525 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP511 INFO-VAR STRM=WP511 INFO=WORK VAR=POWER c 47.7 psi = 110 ft. head F DP511 = 47.7 F AP511 =(FMP511/3600.)/(RMP511*1000.)+(FCP511/3600.)/(RCP511*1000.) c Recirculation Ratio = 3 F AP511 = AP511 * (3. + 1.) F WRITE(NHSTRY,*)' AP511 = ',ap511 F WP511 =(AP511 * (DP511*6894.8) / (EPM*EEL) ) / 1000. ; P-512 2ND Effect Pump DEFINE FMP512 STREAM-VAR STRM=528 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP512 STREAM-VAR STRM=528 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP512 STREAM-VAR STRM=528 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP512 STREAM-VAR STRM=528 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP512 INFO-VAR STRM=WP512 INFO=WORK VAR=POWER c 47.7 psi = 110 ft. head F DP512 = 47.7 F AP512 =(FMP512/3600.)/(RMP512*1000.)+(FCP512/3600.)/(RCP512*1000.) c Recirculation Ratio = 1.9 F AP512 = AP512 * (1.9 + 1.) F WRITE(NHSTRY,*)' AP512 = ',ap512 F WP512 =(AP512 * (DP512*6894.8) / (EPM*EEL) ) / 1000. ; P-513 3RD Effect Pump DEFINE FMP513 STREAM-VAR STRM=531 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP513 STREAM-VAR STRM=531 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP513 STREAM-VAR STRM=531 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP513 STREAM-VAR STRM=531 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP513 INFO-VAR STRM=WP513 INFO=WORK VAR=POWER c 47.7 psi = 110 ft. head F DP513 = 47.7 F AP513 =(FMP513/3600.)/(RMP513*1000.)+(FCP513/3600.)/(RCP513*1000.) c Recirculation Ratio = 3 F AP513 = AP513 * (3. + 1.) F WRITE(NHSTRY,*)' AP513 = ',ap513 F WP513 =(AP513 * (DP513*6894.8) / (EPM*EEL) ) / 1000. ; P-514 CONDENSATE Pump DEFINE FMP514 STREAM-VAR STRM=534A SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP514 STREAM-VAR STRM=534A SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP514 STREAM-VAR STRM=534A SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP514 STREAM-VAR STRM=534A SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP514 INFO-VAR STRM=WP514 INFO=WORK VAR=POWER c 47.7 psi = 110 ft. head F DP514 = 47.7 F AP514 =(FMP514/3600.)/(RMP514*1000.)+(FCP514/3600.)/(RCP514*1000.) F WP514 =(AP514 * (DP514*6894.8) / (EPM*EEL) ) / 1000. ; P-515 Scrubber Bottoms Pump DEFINE FMP515 STREAM-VAR STRM=551 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP515 STREAM-VAR STRM=551 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP515 STREAM-VAR STRM=551 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP515 STREAM-VAR STRM=551 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP515 INFO-VAR STRM=WP515 INFO=WORK VAR=POWER c 47.7 psi = 110 ft. head F DP515 = 47.7 F AP515 =(FMP515/3600.)/(RMP515*1000.)+(FCP515/3600.)/(RCP515*1000.) F WP515 =(AP515 * (DP515*6894.8) / (EPM*EEL) ) / 1000. ; P-530 Recycle Water Pump DEFINE FMP530 STREAM-VAR STRM=572 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP530 STREAM-VAR STRM=572 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP530 STREAM-VAR STRM=572 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP530 STREAM-VAR STRM=572 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP530 INFO-VAR STRM=WP530 INFO=WORK VAR=POWER c 68 psi = 150 ft head F DP530 = 68. F AP530 =(FMP530/3600.)/(RMP530*1000.)+(FCP530/3600.)/(RCP530*1000.) F WP530 =((AP530) * (DP530*6894.8) / (EPM*EEL) ) / 1000. ; P-602 Anaerobic Digester Feed Pump DEFINE FMP602 STREAM-VAR STRM=613 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP602 STREAM-VAR STRM=613 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP602 STREAM-VAR STRM=613 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP602 STREAM-VAR STRM=613 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP602 INFO-VAR STRM=WP602 INFO=WORK VAR=POWER c 68 psi = 150 ft. head F DP602 = 68. F AP602 =(FMP602/3600.)/(RMP602*1000.)+(FCP602/3600.)/(RCP602*1000.) F WP602 =(AP602 * (DP602*6894.8) / (EPM*EEL) ) / 1000. ; P-606 Aerobic Digester Feed Pump DEFINE FMP606 STREAM-VAR STRM=618 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP606 STREAM-VAR STRM=618 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP606 STREAM-VAR STRM=618 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP606 STREAM-VAR STRM=618 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP606 INFO-VAR STRM=WP606 INFO=WORK VAR=POWER c 68 psi = 150 ft head F DP606 = 68. F AP606 =(FMP606/3600.)/(RMP606*1000.)+(FCP606/3600.)/(RCP606*1000.) F WP606 =(AP606 * (DP606*6894.8) / (EPM*EEL) ) / 1000. ; P-608 Return Activated Sludge pump DEFINE FMP610 STREAM-VAR STRM=625 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP610 STREAM-VAR STRM=625 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP610 STREAM-VAR STRM=625 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP610 STREAM-VAR STRM=625 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP608 INFO-VAR STRM=WP608 INFO=WORK VAR=POWER c FAC608 is the recycle ratio on stream 625 F FAC608 = 1. c 68 PSI = 150 ft. head F DP608 = 68. F AP608 =(FMP610/3600.)/(RMP610*1000.)+(FCP610/3600.)/(RCP610*1000.) F WP608 =(FAC608 * AP608 * (DP608*6894.8) / (EPM*EEL) ) / 1000. ; P-610 Waste Activated Sludge Pump DEFINE WP610 INFO-VAR STRM=WP610 INFO=WORK VAR=POWER c 40 PSI = 92 ft. head F DP610 = 40. F AP610 =(FMP610/3600.)/(RMP610*1000.)+(FCP610/3600.)/(RCP610*1000.) F WP610 =(AP610 * (DP610*6894.8) / (EPM*EEL) ) / 1000. ; P-611 Clarifier feed Pump DEFINE FMP611 STREAM-VAR STRM=621 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP611 STREAM-VAR STRM=621 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP611 STREAM-VAR STRM=621 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP611 STREAM-VAR STRM=621 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP611 INFO-VAR STRM=WP611 INFO=WORK VAR=POWER F DP611 = 68.0 F AP611 =(FMP611/3600.)/(RMP611*1000.)+(FCP611/3600.)/(RCP611*1000.) F WP611 =(AP611 * (DP611*6894.8) / (EPM*EEL) ) / 1000. F WRITE(NHSTRY,*)'AP611=',AP611,'WP611=',WP611 ; P-614 Filtrate/Wash Recycle Pump DEFINE FMP614 STREAM-VAR STRM=627 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP614 STREAM-VAR STRM=627 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP614 STREAM-VAR STRM=627 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP614 STREAM-VAR STRM=627 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP614 INFO-VAR STRM=WP614 INFO=WORK VAR=POWER F DP614 = 68.0 F AP614 =(FMP614/3600.)/(RMP614*1000.)+(FCP614/3600.)/(RCP614*1000.) F WP614 =(AP614 * (DP614*6894.8) / (EPM*EEL) ) / 1000. ; P-616 Potable Water Pump DEFINE FMP616 STREAM-VAR STRM=624 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP616 STREAM-VAR STRM=624 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP616 STREAM-VAR STRM=624 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP616 STREAM-VAR STRM=624 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP616 INFO-VAR STRM=WP616 INFO=WORK VAR=POWER ; 68 psi = 150 ft. head F DP616 = 68. F AP616 =(FMP616/3600.)/(RMP616*1000.)+(FCP616/3600.)/(RCP616*1000.) F WP616 =(AP616 * (DP616*6894.8) / (EPM*EEL) ) / 1000. ; P-701 Ethanol Product Pump DEFINE FMP701 STREAM-VAR STRM=515 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP701 STREAM-VAR STRM=515 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP701 STREAM-VAR STRM=515 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP701 STREAM-VAR STRM=515 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP701 INFO-VAR STRM=WP701 INFO=WORK VAR=POWER c 49 psi = 112 ft head F DP701 = 49. F AP701 =(FMP701/3600.)/(RMP701*1000.)+(FCP701/3600.)/(RCP701*1000.) F WP701 =(AP701 * (DP701*6894.8) / (EPM*EEL) ) / 1000. ; P-703 Sulfuric Acid Pump DEFINE FMP703 STREAM-VAR STRM=710 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP703 STREAM-VAR STRM=710 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP703 STREAM-VAR STRM=710 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP703 STREAM-VAR STRM=710 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP703 INFO-VAR STRM=WP703 INFO=WORK VAR=POWER c 65. psi = 150 ft head F DP703 = 65. F AP703 =(FMP703/3600.)/(RMP703*1000.)+(FCP703/3600.)/(RCP703*1000.) F WP703 =(AP703 * (DP703*6894.8) / (EPM*EEL) ) / 1000. ;; P-704 Firewater Pump -- Commented out, because it does not run regularly ; DEFINE FMP704 STREAM-VAR STRM=713 SUBSTREAM=MIXED VAR=MASS-FLOW ; DEFINE RMP704 STREAM-VAR STRM=713 SUBSTREAM=MIXED VAR=MASS-DENSITY ; DEFINE FCP704 STREAM-VAR STRM=713 SUBSTREAM=CISOLID VAR=MASS-FLOW ; DEFINE RCP704 STREAM-VAR STRM=713 SUBSTREAM=CISOLID VAR=MASS-DENSITY ; DEFINE WP704 INFO-VAR STRM=WP704 INFO=WORK VAR=POWER ;c 36 psi = 82 ft head ;F DP704 = 36. ;F AP704 =(FMP704/3600.)/(RMP704*1000.)+(FCP704/3600.)/(RCP704*1000.) ;F WP704 =(AP704 * (DP704*6894.8) / (EPM*EEL) ) / 1000. ; P-706 Ammonia Pump DEFINE FMP706 STREAM-VAR STRM=717 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP706 STREAM-VAR STRM=717 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP706 STREAM-VAR STRM=717 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP706 STREAM-VAR STRM=717 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP706 INFO-VAR STRM=WP706 INFO=WORK VAR=POWER c 10 psi = 22 ft head F DP706 = 10. F AP706 =(FMP706/3600.)/(RMP706*1000.)+(FCP706/3600.)/(RCP706*1000.) F WP706 =(AP706 * (DP706*6894.8) / (EPM*EEL) ) / 1000. ; P-707 Antifoam Pump DEFINE FMP707 STREAM-VAR STRM=417 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP707 STREAM-VAR STRM=417 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP707 STREAM-VAR STRM=417 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP707 STREAM-VAR STRM=417 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP707 INFO-VAR STRM=WP707 INFO=WORK VAR=POWER c 39 psi = 90 ft head F DP707 = 39. F AP707 =(FMP707/3600.)/(RMP707*1000.)+(FCP707/3600.)/(RCP707*1000.) F WP707 =(AP707 * (DP707*6894.8) / (EPM*EEL) ) / 1000. ; P-708 Diesel Pump (no longer needed because it's a propane tank now) DEFINE FMP708 STREAM-VAR STRM=723 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP708 STREAM-VAR STRM=723 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP708 STREAM-VAR STRM=723 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP708 STREAM-VAR STRM=723 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP708 INFO-VAR STRM=WP708 INFO=WORK VAR=POWER c 51.6 psi = 119 ft head ;F DP708 = 51.6 F DP708 = 0.0 F AP708 =(FMP708/3600.)/(RMP708*1000.)+(FCP708/3600.)/(RCP708*1000.) F WP708 =(AP708 * (DP708*6894.8) / (EPM*EEL) ) / 1000. ; P-710 Gasoline Pump DEFINE FMP710 STREAM-VAR STRM=701 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP710 STREAM-VAR STRM=701 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP710 STREAM-VAR STRM=701 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP710 STREAM-VAR STRM=701 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP710 INFO-VAR STRM=WP710 INFO=WORK VAR=POWER c 86.7 psi = 200 ft head F DP710 = 86.7 F AP710 =(FMP710/3600.)/(RMP710*1000.)+(FCP710/3600.)/(RCP710*1000.) F WP710 =(AP710 * (DP710*6894.8) / (EPM*EEL) ) / 1000. ; P-720 CSL Pump DEFINE FMP720 STREAM-VAR STRM=735 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP720 STREAM-VAR STRM=735 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP720 STREAM-VAR STRM=735 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP720 STREAM-VAR STRM=735 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP720 INFO-VAR STRM=WP720 INFO=WORK VAR=POWER c 65 psi = 150 ft head F DP720 = 65. F AP720 =(FMP720/3600.)/(RMP720*1000.)+(FCP720/3600.)/(RCP720*1000.) F WP720 =(AP720 * (DP720*6894.8) / (EPM*EEL) ) / 1000. ; P-750 Cellulase Enzyme Pump DEFINE FMP750 STREAM-VAR STRM=750 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP750 STREAM-VAR STRM=750 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP750 STREAM-VAR STRM=750 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP750 STREAM-VAR STRM=750 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP750 INFO-VAR STRM=WP750 INFO=WORK VAR=POWER c 21.7 psi = 50 ft head F DP750 = 21.7 F AP750 =(FMP750/3600.)/(RMP750*1000.)+(FCP750/3600.)/(RCP750*1000.) F WP750 =(AP750 * (DP750*6894.8) / (EPM*EEL) ) / 1000. ; P-760 CSL/DAP Pump DEFINE FMP760 STREAM-VAR STRM=735 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP760 STREAM-VAR STRM=735 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP760 STREAM-VAR STRM=735 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP760 STREAM-VAR STRM=735 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP760 INFO-VAR STRM=WP760 INFO=WORK VAR=POWER c 65 psi = 150 ft head F DP760 = 65. F AP760 =(FMP760/3600.)/(RMP760*1000.)+(FCP760/3600.)/(RCP760*1000.) F WP760 =(AP760 * (DP760*6894.8) / (EPM*EEL) ) / 1000. ; P-804 Condensate Pump DEFINE FMP804 STREAM-VAR STRM=824 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP804 STREAM-VAR STRM=824 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP804 STREAM-VAR STRM=824 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RCP804 STREAM-VAR STRM=824 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP804 INFO-VAR STRM=WP804 INFO=WORK VAR=POWER c 65 psi = 150 ft head F DP804 = 65. F AP804 =(FMP804/3600.)/(RMP804*1000.)+(FCP804/3600.)/(RCP804*1000.) F WP804 =(AP804 * (DP804*6894.8) / (EPM*EEL) ) / 1000. ; P-828 Blowdown Pump DEFINE FMP828 STREAM-VAR STRM=821 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP828 STREAM-VAR STRM=821 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FCP828 STREAM-VAR STRM=821 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE WP828 INFO-VAR STRM=WP828 INFO=WORK VAR=POWER DEFINE RCP828 STREAM-VAR STRM=821 SUBSTREAM=CISOLID VAR=MASS-DENSITY c 65 psi = 150 ft head F DP828 = 65 F AP828 =(FMP828/3600.)/(RMP828*1000.)+(FCP828/3600.)/(RCP828*1000.) F WP828 =(AP828 * (DP828*6894.8) / (EPM*EEL) ) / 1000. ; P-830 Hydrazine addition - flow set as 0.001 of 813 DEFINE FMP830 STREAM-VAR STRM=813 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RMP830 STREAM-VAR STRM=813 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE WP830 INFO-VAR STRM=WP830 INFO=WORK VAR=POWER c FR830 is the ratio of hydrazine flow to stream 813 (0.001 is a guess) F FR830=0.001 c 33 psi = 75 ft head F DP830 = 33. F AP830 =(FR830*FMP830/3600.)/(RMP830*1000.) F WP830 =(AP830 * (DP830*6894.8) / (EPM*EEL) ) / 1000. ; P-902 Cooling Water Pump DEFINE FM902 STREAM-VAR STRM=940 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RM902 STREAM-VAR STRM=940 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FC902 STREAM-VAR STRM=940 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RC902 STREAM-VAR STRM=940 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP902 INFO-VAR STRM=WP902 INFO=WORK VAR=POWER c 30 psi = 70 ft head F DP902 = 30. F AP902=(FM902/3600.)/(RM902*1000.) F & +(FC902/3600.)/(RC902*1000.) F WP902=(AP902 * (DP902*6894.8) / (EPM*EEL) ) / 1000. ; P-912 Makeup Water Pump DEFINE FM912 STREAM-VAR STRM=904 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RM912 STREAM-VAR STRM=904 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FC912 STREAM-VAR STRM=904 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RC912 STREAM-VAR STRM=904 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP912 INFO-VAR STRM=WP912 INFO=WORK VAR=POWER c 33 psi = 75 ft head F DP912 = 33. F AP912=(FM912/3600.)/(RM912*1000.) F & +(FC912/3600.)/(RC912*1000.) F WP912=(AP912 * (DP912*6894.8) / (EPM*EEL) ) / 1000. ; P-914 Process Water Circulating Pump DEFINE FM914 STREAM-VAR STRM=905 SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RM914 STREAM-VAR STRM=905 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE FC914 STREAM-VAR STRM=905 SUBSTREAM=CISOLID VAR=MASS-FLOW DEFINE RC914 STREAM-VAR STRM=905 SUBSTREAM=CISOLID VAR=MASS-DENSITY DEFINE WP914 INFO-VAR STRM=WP914 INFO=WORK VAR=POWER c 65 psi = 150 ft head F DP914 = 65. F AP914=(FM914/3600.)/(RM914*1000.) F & +(FC914/3600.)/(RC914*1000.) F WP914=(AP914 * (DP914*6894.8) / (EPM*EEL) ) / 1000. READ-VARS SSFVES QREB & FMP201 RMP201 FCP201 RCP201 & STC220 F256 & FMP209 RMP209 FCP209 RCP209 & FMP222 RMP222 FCP222 RCP222 & FMP224 RMP224 FCP224 RCP224 & FMP211 FCP211 & FMP239 RMP239 FCP239 RCP239 & FMP310 RMP310 FCP310 RCP310 & FMP300 RMP300 FCP300 RCP300 & FMP301 RMP301 FCP301 RCP301 & FMP400 RMP400 FCP400 RCP400 & FMP405 RMP405 FCP405 RCP405 & FMP420 RMP420 FCP420 RCP420 & FMP501 RMP501 FCP501 RCP501 & FMP504 RMP504 FCP504 RCP504 & FMP511 RMP511 FCP511 RCP511 & FMP512 RMP512 FCP512 RCP512 & FMP513 RMP513 FCP513 RCP513 & FMP514 RMP514 FCP514 RCP514 & FMP515 RMP515 FCP515 RCP515 & FMP530 RMP530 FCP530 RCP530 & FMP602 RMP602 FCP602 RCP602 & FMP606 RMP606 FCP606 RCP606 & FMP610 RMP610 FCP610 RCP610 & FMP614 RMP614 FCP614 RCP614 & FMP616 RMP616 FCP616 RCP616 & FMP701 RMP701 FCP701 RCP701 & FMP703 RMP703 FCP703 RCP703 & FMP706 RMP706 FCP706 RCP706 & FMP707 RMP707 FCP707 RCP707 & FMP708 RMP708 FCP708 RCP708 & FMP710 RMP710 FCP710 RCP710 & FMP720 RMP720 FCP720 RCP720 & FMP750 RMP750 FCP750 RCP750 & FMP760 RMP760 FCP760 RCP760 & FMP804 RMP804 FCP804 RCP804 & FMP828 RMP828 FCP828 RCP828 & FMP830 RMP830 & FM902 RM902 FC902 RC902 & FM912 RM912 FC912 RC912 & FM914 RM914 FC914 RC914 WRITE-VARS WP201 WP205 AWP209 WP211 WP222 WP224 & WP239 WP213 & WP300 WP301 WP302 WP306 WP310 & WP400 WP405 WP420 & WP501 WP503 WP504 WP505 WP511 WP512 WP513 WP514 WP515 & WP530 WP602 WP606 WP608 WP610 WP614 WP616 & WP701 WP703 WP706 WP707 WP708 WP710 WP720 WP750 WP760 & WP804 WP828 WP830 & WP902 WP912 WP914 & P501GP PMPSSF PMPSAC ; EXECUTE BEFORE PMPWK ; FORTRAN MISCPOW ;THIS BLOCK CALCULATES THE POWER REQUIREMENTS FOR ;ALL OF THE SOLIDS HANDLING AND OTHER MISCELLANEOUS ;EQUIPMENT EXCEPT AREA 100 (CALCULATED IN POW101) ; ; ;DEFINE THE POWER REQUIREMENTS ( KW / (KG/HR) ) ;UNLESS OTHERWISE NOTED, THE POWER REQUIREMENTS WERE CALCULATED ;FROM THE 1990 BASE CASE. ;THEY ARE SIMPLY RATIOS OF THE POWER REQUIRED AND THE FLOWRATE ;THROUGH THE EQUIPMENT ITEM. ; ; AREA 200 c PH=Prehydrolysis Screw Feeder / Impregnator / Reactor (M-202) DEFINE ST101 STREAM-PROP STREAM=101 PROPERTY=MASSFLW DEFINE WPH INFO-VAR STREAM=WM202 INFO=WORK VARIABLE=POWER ; ; DELTA-T/SUNDS: ; Power Requirement 0.85 * 1363 hp (motor sizes) = 1158 hp = 863 kW ; for total feed of 159948 kg/hr in Stream 101 ; 863 / 159948 = 5.396E-3 ; ; HARRIS/ANCO-EAGLIN: ; Power Requirement 0.85 * 1801 hp (motor sizes) = 1531 hp = 1142 kW ; for total feed of 159948 kg/hr in Stream 101 ; 1142 / 159948 = 7.138E-3 ; F PH = 7.138E-3 F WPH = PH * ST101 F WRITE(NHSTRY,*)'STRM 101: ',ST101,' WM202: ',WPH ; c FL=Flash Tank Screw Conveyor (C-201) DEFINE STV220 STREAM-VAR STREAM=220 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE STC220 STREAM-VAR STREAM=220 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WFL INFO-VAR STREAM=WC201 INFO=WORK VARIABLE=POWER ; Power Req. 1.643E-4 kW/ kg/hr == 50 hp/ 250 ton/hr F FL=1.643E-4 F WFL=FL*(STV220+STC220) ; c HF=Hydrolysate PneumaPress (S-205) C Power based on the solids flow of stream 220 C DEFINE WHF INFO-VAR STREAM=WS205 INFO=WORK VARIABLE=POWER ; ; Power Required from Harris design (60 hp for 3 machines at 75% power) ; equals 135 hp / Flow from R0101C (see equip design ; sheet) ; Power Required 135 hp / 50299 kg/hr CISOLIDS flow = 2.68E-3 hp/kg/hr ; = 2.00E-3 kW/kg/hr F HF = 2.0E-3 F WHF = HF * STC220 ; c CK=Hydrolysate Washed Solids Belt Conveyor (C-202) DEFINE ST255 STREAM-PROP STREAM=255 PROPERTY=MASSFLW DEFINE WCK INFO-VAR STREAM=WC202 INFO=WORK VARIABLE=POWER c ; Power Required from Harris design (50 hp at 75% power) ; equals 37.5 hp / Flow from R0101C (see equip design ; sheet) ; 37.5 hp/91633 kg/hr = 28.0 KW/91633 Kg/hr ; = 3.06E-4 kW/kg/hr F CK = 3.06e-4 F WCK = CK * ST255 F WRITE(NHSTRY,*)'STRM 255: ',ST255,' WC202: ',WCK ; c GYPREM = Gypsum Filter(S-222) DEFINE ST239 STREAM-PROP STREAM=239 PROPERTY=MASSFLW DEFINE GYPREM INFO-VAR STREAM=WS222 INFO=WORK VARIABLE=POWER ; C 25 HP / 167280 KG/HR = 1.495E-4hp/kg/hr = 1.114E-4 KW/KG/HR ; F GYPREM = 1.114E-4 * ST239 F WRITE(NHSTRY,*)'STRM 239: ',ST239,' WC222: ',GYPREM ; c ULOAD=Lime Unloader blower DEFINE ULOAD INFO-VAR STREAM=WP223 INFO=WORK VARIABLE=POWER DEFINE STC227 STREAM-VAR STREAM=227 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW ; Average Power 8.6 hp / 548 kg/hr ; ; Power Req. 6.4 kW / 548 kg/hr = 0.012 kW / kg/hr ; F UL1=0.012 F ULOAD=UL1*(STC227) ; c FL=Lime Solids Air Lock (C-225) DEFINE WFL2 INFO-VAR STREAM=WC225 INFO=WORK VARIABLE=POWER ; 3.523E-4 kW/ kg/hr =1.5 hp/7000 lb/hr from Icarus 20 Oct 98 F FL2=3.523E-4 F WFL2=FL2*(STC227) ; ; AREA 500 c SVE=Mole Sieve System (T-507-8) ;THE POWER REQUIREMENTS ARE SIMPLE RATIOS FROM A ;COST QUOTE. DEFINE ETHDEN STREAM-VAR STREAM=515 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE ETHFLO STREAM-VAR STREAM=515 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE PWR INFO-VAR STREAM=WM503 INFO=WORK VAR=POWER F GALFLO = (ETHFLO / ETHDEN / 3.7854) F WRITE(NHSTRY,*)'GALFLO,ETHFLO,ETHDEN= ',GALFLO,ETHFLO,ETHDEN c .0204 kW/gal/hr F PWR = GALFLO * 0.0204 F WRITE(NHSTRY,*)'PWR= ',PWR ; c CF=PNEUMAPRESS (S-505) ; was formerly centrifuges so that's why it's CF DEFINE STC570 STREAM-VAR STREAM=570 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WCF INFO-VAR STREAM=WS505 INFO=WORK VAR=POWER c c 180 hp * (.7457 kW/hp) / 26601 kg/hr c F CF = 180. * 0.7457 / 26601. F WCF = CF * STC570 ; c S1=SLUDGE SCREWS (C-501A/B) DEFINE STV5 STREAM-VAR STREAM=571 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE STC5 STREAM-VAR STREAM=571 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WS1 INFO-VAR STREAM=WC501 INFO=WORK VAR=POWER C 85 hp / 99199 Kg/hr F S1 = (85./99199.) * (STV5 + STC5) C Convert to KW F WS1 = S1 * 0.7457 ; AREA 600 c c S2=Digestion Cell Mass Screws (C-614) DEFINE SV614 STREAM-VAR STREAM=623 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SC614 STREAM-VAR STREAM=623 SUBSTREAM=CISOLID & VARIABLE=MASS-FLOW DEFINE WS2 INFO-VAR STREAM=WC614 INFO=WORK VAR=POWER C 7.5 hp / 978 Kg/hr F S2 = (7.5/978.) * (SV614 + SC614) C Convert to KW F WS2 = S2 * 0.7457 c c S3=Finishing Belt Filter Press (S-614) DEFINE ST618 STREAM-PROP STREAM=618 PROPERTY=MASSFLW DEFINE WS3 INFO-VAR STREAM=WS614 INFO=WORK VAR=POWER C C 30 hp * .7457 kW/hp / 185782 kg/hr C F S3 = 30. * 0.7457 / 185782. F WS3 = S3 * ST618 ; C Anerobic Nutrient Feed System (M-604) C Assume a total of 10 hp per 175,000 kg/hr from 613 DEFINE ST613 STREAM-PROP STREAM=613 PROPERTY=MASSFLW DEFINE WM604 INFO-VAR STREAM=WM604 INFO=WORK VAR=POWER C F REQ = 10. *.7457 / 175000. F WM604 = ST613 * REQ ; C Polymer Addition for Anerobic Sludge Filter (M-612) C Assume a total of 5 hp per 5369 kg/hr from 625 DEFINE ST625 STREAM-PROP STREAM=625 PROPERTY=MASSFLW DEFINE WM612 INFO-VAR STREAM=WM612 INFO=WORK VAR=POWER C F REQ = 5. *.7457 / 5369. F WM612 = ST625 * REQ ; C Mechanical Cleaners for Bar Screens (S-600) C Assume a total of 1 hp per 174500 kg/hr from 612 DEFINE ST612 STREAM-PROP STREAM=612 PROPERTY=MASSFLW DEFINE WS600 INFO-VAR STREAM=WS600 INFO=WORK VAR=POWER C F REQ = 1. *.7457 / 174500. F WS600 = ST612 * REQ ; C Clarifier Mixer (T-610) C Assume a total of 5 hp per 174500 kg/hr from 621 DEFINE ST621 STREAM-PROP STREAM=621 PROPERTY=MASSFLW DEFINE WT610 INFO-VAR STREAM=WT610 INFO=WORK VAR=POWER C F REQ = 5. *.7457 / 174500. F WT610 = ST621 * REQ ; ; AREA 700 ; c UNLDAP=DAP Unloader blower (P-755) ; COPY OF WP223 POWER CALCULATION DEFINE UNLDAP INFO-VAR STREAM=WP755 INFO=WORK VARIABLE=POWER DEFINE STC755 STREAM-VAR STREAM=755 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW ; Average Power 8.6 hp / 548 kg/hr ; ; Power Req. 6.4 kW / 548 kg/hr = 0.012 kW / kg/hr ; F UL2=0.012 F UNLDAP=UL2*(STC755) ; ; c FD=DAP Solids Air Lock (C-755) ; COPY OF WC225 POWER CALCULATION DEFINE WFD2 INFO-VAR STREAM=WC755 INFO=WORK VARIABLE=POWER ; 3.523E-4 kW/ kg/hr =1.5 hp/7000 lb/hr from Icarus 20 Oct 98 F FD2=3.523E-4 F WFD2=FD2*(STC755) ; ; AREA 800 c Power for dryer based on ReTec Quote c 30 hp / 8910 lb/hr (evaporated) = 0.00742 hp/ (kg dry/hr) DEFINE WEM801 INFO-VAR STREAM=WM801 INFO=WORK VAR=POWER DEFINE STV6 STREAM-VAR STREAM=851 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW F EM801=0.00742 *.7457 F WEM801=EM801 * STV6 ; c EM804=Combustion Gas Baghouse (M-804) DEFINE WEM804 INFO-VAR STREAM=WM804 INFO=WORK VAR=POWER c 176 kW power requirement from Quote in REI 1999 report F EM804=176.0 F WEM804=EM804 c c EM830=Hydrazine Addition Package (M-830) DEFINE WEM830 INFO-VAR STREAM=WM830 INFO=WORK VAR=POWER c 10 kW power requirement is just a guess (=13 hp) F EM830=10.0 F WEM830=EM830 c c EM832=Ammonia Addition Package (M-832) DEFINE WEM832 INFO-VAR STREAM=WM832 INFO=WORK VAR=POWER c 10 kW power requirement is just a guess (=13 hp) F EM832=10.0 F WEM832=EM832 c c EM834=Phosphate Addition Package (M-834) DEFINE WEM834 INFO-VAR STREAM=WM834 INFO=WORK VAR=POWER c 10 kW power requirement is just a guess (=13 hp) F EM834=10.0 F WEM834=EM834 c ; ; AREA 900 c CT=COOLING TOWER PACKAGE (M-902) DEFINE PCWCAP INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QCWCAP DEFINE WCT INFO-VAR STREAM=WM902 INFO=WORK VAR=POWER c 5 243 hp fans are required for 41,100,000 cal/sec cooling c 2.204E-5 kW / cal/sec = (5 * 243 hp) / 41,100,000 cal/sec F CT=2.204E-5 c Pumping is also required DEFINE FM946 STREAM-VAR STRM=941A SUBSTREAM=MIXED VAR=MASS-FLOW DEFINE RM946 STREAM-VAR STRM=941A SUBSTREAM=MIXED VAR=MASS-DENSITY C EPM is the pump efficiencies C EEL is the motor efficiencies F EPM = 0.60 F EEL = 0.95 ; 44.3 psi=100 ft head F DP946 = 44.3 F AP946 =(FM946/3600.)/(RM946*1000.) F WP946 =(AP946 * (DP946*6894.8) / (EPM*EEL) ) / 1000. F WCT=CT*PCWCAP+WP946 c EM904=Plant and Instrument Air compressor (M-904) DEFINE WEM104 INFO-VAR STREAM=WM904A INFO=WORK VAR=POWER c 93.2 kW = 125 hp & 2 in use F EM904=93.2*2 F WEM104=EM904 c c ES904=Instrument Air Dryer (S-904) DEFINE WES104 INFO-VAR STREAM=WS904 INFO=WORK VAR=POWER c 12 kW ratioed from Delta T F ES904=12 F WES104=ES904*ST101/159948.0 c EM1008=Chilled Water System Calculation (M-908A/S) DEFINE QREF INFO-VAR STREAM=QCHWTOT INFO=HEAT & VARIABLE=DUTY DEFINE QSSF INFO-VAR STREAM=QH914C INFO=HEAT & VARIABLE=DUTY DEFINE CHWSPT BLOCK-VAR BLOCK=QH14BSP SENT=FRAC & VARIABLE=FRAC ID1=QH14BCHW DEFINE WEM108 INFO-VAR STREAM=WM908 INFO=WORK VAR=POWER c 5.327E-4 kW / cal/sec = 1200 hp / 2000 tons refrigeration F EM908=5.327E-4 F WEM108=EM908*(QREF+QSSF*CHWSPT) c c F WRITE(NHSTRY,60)QREF,QSSF,CHWSPT,EM908,WEM108 F 60 FORMAT('MISC RESULTS',/, F 1 'QREF=',G12.5,/, F 2 'QSSF=',G12.5,/, F 4 'CHWSPT=',G12.5,/, F 6 'EM908=',G12.5,/, F 7 'WEM108=',G12.5) c EM910=CIP System Calculation (M-910) c I entered the required power from Delta-T and allowed it to be ratioed to c the flow of 914 DEFINE WCIP INFO-VAR STREAM=WM910 INFO=WORK VAR=POWER c Pumping is required DEFINE FM914 STREAM-VAR STRM=914 SUBSTREAM=MIXED VAR=MASS-FLOW C EPM is the pump efficiencies C EEL is the motor efficiencies ; First pump 600 gpm & 125 psi from Delta-T F DPPMP1 = 125.0 F APPMP1 = 600.0 / 60 * 3.785 / 1000 F WPPMP1 =(APPMP1 * (DPPMP1*6894.8) / (EPM*EEL) ) / 1000. ; Second pump 2000 gpm & 60 psi from Delta-T F DPPMP2 = 60.0 F APPMP2 = 2000.0 / 60 * 3.785 / 1000 F WPPMP2 =(APPMP2 * (DPPMP2*6894.8) / (EPM*EEL) ) / 1000. ; Third pump 600 gpm from Delta-T & 60 psi MR estimate F DPPMP3 = 60.0 F APPMP3 = 600.0 / 60 * 3.785 / 1000 F WPPMP3 =(APPMP3 * (DPPMP3*6894.8) / (EPM*EEL) ) / 1000. ; Agitator in Sterizilation Tank c 1 hp / 1000 gal MR estimate c 50000 gal Delta T F WPAG1 = 1 * 50000/1000 * 0.7457 ; Agitator in Cleaning Chemical Tank c 0.5 hp / 1000 gal MR estimate c 50000 gal Delta T F WPAG2 = 0.5 * 50000/1000 * 0.7457 ; Centrifugal Separator c 25 kW MR estimate F WPCN1 = 25 c Total power is ratioed to flow of 914 (63 was design flow) F WCIP = (WPPMP1+WPPMP2+WPPMP3+WPAG1+WPAG2+WPCN1)*FM914/63.0 c EXECUTE AFTER POWER ; ; FORTRAN PLANTPOW DEFINE POWREQ INFO-VAR STREAM=WPLNTPOW INFO=WORK & VARIABLE=POWER c 1000 kW requirement is a guess (MR 12 Feb 1998) F POWREQ=1000 EXECUTE AFTER MISCPOW ; FORTRAN AIRREQ ;F COMMON /CLSSET/ CLYLD, CLPROD, CLVES, CLVOL, CLWV DEFINE CLYLD PARAMETER 41 DEFINE CLPROD PARAMETER 42 DEFINE CLVES PARAMETER 43 DEFINE CLVOL PARAMETER 44 DEFINE CLWV PARAMETER 45 ; ;CONTROLS THE AMOUNT OF AIR NEEDED IN CELLULASE ;PRODUCTION AND SEED FERMENTORS ; ; DEFINE STIN STREAM-VAR STREAM=413 SUBSTREAM=MIXED & ; VARIABLE=MASS-FLOW ;STIN IS ALSO DV1 DEFINE STDEN STREAM-VAR STREAM=413 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY ; DEFINE ARFIN STREAM-VAR STREAM=432 SUBSTREAM=MIXED & ; VARIABLE=MASS-FLOW ;ARFIN IS ALSO DV2 DEFINE ARFDEN STREAM-VAR STREAM=432 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE SDIN STREAM-VAR STREAM=431 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE SDDEN STREAM-VAR STREAM=431 SUBSTREAM=MIXED & VARIABLE=MASS-DENSITY DEFINE CL412A MASS-FLOW STREAM=412A SUBSTREAM=CISOLID & COMPONENT=CELLULOS DEFINE XY412A MASS-FLOW STREAM=412A SUBSTREAM=MIXED & COMPONENT=XYLOSE DEFINE AIRIN STREAM-VAR STREAM=440 SUBSTREAM=MIXED & VARIABLE=MASS-FLOW DEFINE F1 BLOCK-VAR BLOCK=ASPLT SENT=FRAC VARIABLE=FRAC & ID1=413 ; CLYLD IS THE CELLULASE YIELD (FPU/G CELLULOSE + G XYLOSE) ; AND IS ENTERED IN SETVAR ; CLPROD IS THE CELLULASE PRODUCTION PRODUCTIVITY (FPU/L HR) ; AND IS ENTERED IN SETVAR c WORKING VOLUME (WV1)=90% ; IS ENTERED IN SETVAR (CLWV) c AIR REQUIRED IN PRODUCTION FERMENTORS (AIR1) = 0.577 VVM c 0.577 VVM = OTR OF 75 mMOL/L HR & 20% DO F AIR1=0.577 c V1 is the volume (in liters) of the production ferms c it is calculated from the flow rates, yield, and productivity c 2*CLVOL is added for the 2 ferms not in use. F V1=((CL412A+XY412A)*1000*CLYLD/CLPROD)/CLWV F DV1=STDEN*(V1*60*AIR1) c CLVES is the number of production vessels and is calculated here F CLVES=V1/CLVOL + 3. c c RESIDENCE TIME IN SEED FERMENTORS=3.5 DAYS c TOTAL TURNAROUND TIME (T2)=4.0 DAYS F T2=72.0 c VOLUME (WV2)=90% F WV2=0.8 c AIR REQUIRED IN SEED FERMENTORS = 0.577 VVM c 0.577 VVM = OTR OF 75 mMOL/L HR & 20% DO FOR PRODUCTION FERMS c MAY BE SLIGHTLY HIGHER FOR SEEDS F AIR2=0.577 c NUMBER OF SEED TRAINS (SEED) = 2 F SEED=2 c VOLUMETRIC FLOWRATE OF SUBSTRATE INTO THE SEED FERMENTORS IS VFL2 F VFL2=SDIN/SDDEN F DV2=ARFDEN*(VFL2*T2*60*AIR2*seed)/WV2 c F F1=DV1/(DV1+DV2) c CALCULATE TOTAL AIR IN"D:\GJK\enz998\G9809G.HIS" F AIRIN=DV1 + DV2 c F WRITE(NHSTRY,80)STDEN,V1,DV1,ARFIN,ARFDEN,SDIN, F 1 SDDEN,AIRIN,F1,CLVES F 80 FORMAT('AIRREQ RESULTS',/, F 2 'STDEN ',G12.5,/, F 3 'V1 ',G12.5,/, F 4 'DV1 ',G12.5,/, F 5 'ARFIN ',G12.5,/, F 6 'ARFDEN ',G12.5,/, F 7 'SDIN ',G12.5,/, F 8 'SDDEN ',G12.5,/, F 9 'AIRIN ',G12.5,/, F 1 'F1 ',G12.5,/, F 2 'CLVES ',G12.5) READ-VARS STDEN ARFDEN SDIN SDDEN CL412A XY412A CLYLD CLPROD CLVOL CLWV WRITE-VARS AIRIN F1 CLVES ; EXECUTE BEFORE ACOMP ; FORTRAN WATERDEM ; ;THIS BLOCK CALCULATES THE TOTAL WELL WATER DEMAND FOR THE ;ENTIRE PROCESS. ;PWMU IS PROCESS H2O MAKE-UP. CTL IS COOLING TOWER LOSSES. ;STLOSS ARE LOSSES FROM THE STEAM SYSTEM, INCLUDING DIRECT ;STEAM INJECTION & BOILER BLOWDOWN. CIPCS ARE LOSSES FROM ; THE CIP/CS SYSTEM. CW IS THE COOLING TOWER STREAM. ; Include water to IX DEFINE PWMU STREAM-VAR STREAM=574 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE STLOSS STREAM-VAR STREAM=811 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; Read Variable - Additional Stream to reduce flow of 535 to Digestor DEFINE EXTRA STREAM-VAR STREAM=251 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; Write variable - amount of well water mixed with treated water DEFINE WELLMX STREAM-VAR STREAM=943 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE WATI STREAM-VAR STREAM=903 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE TRTWW STREAM-VAR STREAM=624 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE SCRBWT STREAM-VAR STREAM=524 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE CWMKUP STREAM-VAR STREAM=941 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE CIPCS STREAM-VAR STREAM=906 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; ;CIP/CS LOSS IS SET AT 320 LB/HR BY THE BASE CASE. ; F CIPCS=145 c F WATI = PWMU + STLOSS + CIPCS + CWMKUP - TRTWW + SCRBWT F 1 - EXTRA F WELLMX = WATI - STLOSS - SCRBWT c ;F write(nhstry,50)CWEVAP,CWWNDG,CWBL2,CWBL1,CIPCS,SCRBWT,PWMU, ;F 1 STLOSS,TRTWW,WELLMX,WATI,CWTOT ;F 50 format(' WATER RESULTS',/, ;F 9 ' CWEVAP(Cooling Tower Evap, Calc) = ',g12.5,/, ;F 1 ' CWWNDG(Cooling Tower Windage) = ',g12.5,/, ;F 6 ' CWBL2(Cooling Tower Blowdown, Calc Here) = ',g12.5,/, ;F 6 ' CWBL1(Cooling Tower Blowdown, Specified) = ',g12.5,/, ;F 2 ' CIPCS(CIP/CS Loses - Fixed) = ',g12.5,/, ;F 4 ' SCRBWT(Scrubber water demand) = ',g12.5,/, ;F 3 ' PWMU(Main make-up water #574) = ',g12.5,/, ;F 4 ' STLOSS(Steam Losses #811) = ',g12.5,/, ;F 7 ' TRTWW(Treated WW) = ',g12.5,/, ;f 8 ' WELLMX(Well water mixed with treated) = ',g12.5,/, ;F 5 ' WATI(Total #903) = ',g12.5,/, ;f 6 ' cwtot = ',g12.5) ; READ-VARS PWMU STLOSS TRTWW SCRBWT EXTRA CWMKUP WRITE-VARS WATI WELLMX CIPCS ; EXECUTE BEFORE T914 ; FORTRAN CWDEM ; ;THIS BLOCK CALCULATES THE TOTAL WELL WATER DEMAND FOR THE ;ENTIRE PROCESS. ;PWMU IS PROCESS H2O MAKE-UP. CTL IS COOLING TOWER LOSSES. ;STLOSS ARE LOSSES FROM THE STEAM SYSTEM, INCLUDING DIRECT ;STEAM INJECTION & BOILER BLOWDOWN. CIPCS ARE LOSSES FROM ; THE CIP/CS SYSTEM. CW IS THE COOLING TOWER STREAM. ; Read Variable - total flow to Cooling tower DEFINE CWTOT STREAM-VAR STREAM=946 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; Read Variable - Evaporative Loss DEFINE CWEVAP STREAM-VAR STREAM=949 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; Read Variable - Specified Value of Blowdown DEFINE CWBL1 STREAM-VAR STREAM=944 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; Calculated value of Blowdown DEFINE CWBL2 STREAM-VAR STREAM=944A SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; Total Cooling Tower Make-up DEFINE CWMKUP STREAM-VAR STREAM=941 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE CWWNDG STREAM-VAR STREAM=942 SUBSTREAM=MIXED VARIABLE=MASS-FLOW ; c Windage is assumed to be 0.1% of the total flow to the tower (946) c Blowdown is assumed to be equal to the evap loss + windage with c 90% being recovered to the tower (10% loss needing makeup) c F CWWNDG = 0.001 * CWTOT F CWBL2 = 0.1 * (CWWNDG + CWEVAP) f CWBL1 = CWBL2 F CWMKUP = CWBL2 + CWWNDG + CWEVAP c READ-VARS CWEVAP CWTOT WRITE-VARS CWBL2 CWMKUP CWWNDG CWBL1 ; ;FORTRAN FLOW840 ;; This Fortran block scales the flow of 840A substreams from ;; a specified overall flowrate (variable FL840). ;; The definition of the biomass fractions is picked up from the ;; original Stream 840 definition. ; DEFINE CH4840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED & ; COMPONENT=CH4 ; DEFINE H2O840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED & ; COMPONENT=H2O ; DEFINE SSL840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED & ; COMPONENT=SOLSLDS ; DEFINE EXT840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED & ; COMPONENT=EXTRACT ; DEFINE PRT840 MASS-FLOW STREAM=840 SUBSTREAM=MIXED & ; COMPONENT=PROTEIN ; DEFINE SOL840 STREAM-VAR STREAM=840 SUBSTREAM=CISOLID & ; VARIABLE=MASS-FLOW ;c FL840 is the total desired flow of 840 ;c (Input by user here) ;F FL840=1 ;C ;C Calculate the various fractions in 840 based upon definition in 840 ;F TFL840 = CH4840 + H2O840 + SSL840 + EXT840 + PRT840 + SOL840 ;F RATIO = FL840/TFL840 ;c ;F CH4840 = CH4840 * RATIO ;F SOL840 = SOL840 * RATIO ;F SSL840 = SSL840 * RATIO ;F EXT840 = EXT840 * RATIO ;F PRT840 = PRT840 * RATIO ;F H2O840 = H2O840 * RATIO ;; EXECUTE BEFORE M803CMB ; READ-VARS CH4840 H2O840 SSL840 EXT840 PRT840 SOL840 ; WRITE-VARS CH4840 H2O840 SSL840 EXT840 PRT840 SOL840 ; SENSITIVITY MASSFLOW F COMMON /WWLOAD/ CODTOT, BODTOT, CODDAY, BODDAY F COMMON /WWLOD2/ COD2, BOD2, CODDY2, BODDY2, BODHP ; DEFINE AA220 MOLE-FLOW STREAM=220 SUBSTREAM=MIXED COMPONENT=AACID DEFINE DD501 BLOCK-VAR BLOCK=D501 VARIABLE=DIAM SENTENCE=TSIZE-RESULT ID1=1 DEFINE HLETOT PARAMETER 2 DEFINE WATCON PARAMETER 3 DEFINE BTU101 PARAMETER 4 DEFINE P501GP PARAMETER 5 DEFINE SSFVES PARAMETER 31 DEFINE SACVES PARAMETER 36 DEFINE CLPROD PARAMETER 42 DEFINE CLVES PARAMETER 43 DEFINE PS0506 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QCD501 DEFINE PS0511 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QCD502 DEFINE QCWCAP INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QCWCAP DEFINE QF300A INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QF300A DEFINE QF0300 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QF300 DEFINE QF0400 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QF400 DEFINE S221 STREAM-PROP STREAM=221 PROPERTY=MASSFLW DEFINE S256 STREAM-PROP STREAM=256 PROPERTY=MASSFLW DEFINE S510 STREAM-PROP STREAM=510 PROPERTY=MASSFLW DEFINE S521 STREAM-PROP STREAM=521 PROPERTY=MASSFLW DEFINE S851 STREAM-PROP STREAM=851 PROPERTY=MASSFLW ; AREA 100 WORK STREAMS DEFINE WP101 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP101 DEFINE WP102 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP102 DEFINE WP103 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP103 DEFINE WP104 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP104 DEFINE WP105 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP105 DEFINE WC101 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC101 DEFINE WC102 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC102 DEFINE WC104 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC104 DEFINE WC103 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC103 DEFINE WM104 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM104 DEFINE WM105 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM105 DEFINE WM107 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM107 DEFINE WS101 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS101 DEFINE WS102 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS102 ;Calculates the work for area 100 F C100 = WC101+WC102+WC104+WC103 F M100 = WM104+WM105+WM107+WP101+WP102+WP103+WP104+WP105 F S100 = WS101+WS102 F WA100= C100+M100+S100 ; AREA 200 WORK STREAMS DEFINE WC201 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC201 DEFINE WM202 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM202 DEFINE WP201 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP201 DEFINE WC202 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC202 DEFINE WM205 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM205 DEFINE WP205 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP205 DEFINE WP211 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP211 DEFINE WP213 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP213 DEFINE WP224 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP224 DEFINE WS205 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS205 DEFINE WS221 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS221 DEFINE WT205 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT205 DEFINE WT232 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT232 DEFINE WC225 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC225 DEFINE WP209 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP209 DEFINE WP222 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP222 DEFINE WP223 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP223 DEFINE WP239 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP239 DEFINE WS222 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS222 DEFINE WT209 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT209 DEFINE WT224 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT224 ;Calculates the work for area 200 F C200 = WC201+WM202+WP201+WC202+WM205+WP205+WP211+WP213 F 1 +WP224 F M200 = WS205+WS221+WT205+WT232+WC225+WP209+WP222+WP223 F 2 +WP239 ;Hot Wash Blowdown Pump +WP228 F S200 = WS222+WT209+WT224 F WA200=C200+M200+S200 ; AREA 300 WORK STREAMS DEFINE WP301 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP301 DEFINE WP302 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP302 DEFINE WT301 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT301 DEFINE WT304 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT304 DEFINE WT305 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT305 DEFINE WP300 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP300 DEFINE WP306 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP306 DEFINE WP310 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP310 DEFINE WT300 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT300 DEFINE WT306 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT306 DEFINE WT310 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT310 ;Calculates the work for area 300 F C300 = WP301+WP302+WT301+WT304+WT305 F M300 = WP300+WP306+WP310 F S300 = WT300+WT306+WT310 F WA300=C300+M300+S300 ; AREA 400 WORK STREAMS DEFINE WP401 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP401 DEFINE WT402 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT402-3 DEFINE WM401 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM401 DEFINE WP400 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP400 DEFINE WP405 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP405 DEFINE WP420 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP420 DEFINE WT400 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT400 DEFINE WT405 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT405 ;Calculates the work for area 400 F C400 = WP401+WT402+WM401 F M400 = WP400+WP405+WP420 F S400 = WT400+WT405 F WA400=C400+M400+S400 ; AREA 500 WORK STREAMS DEFINE WC501 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC501 DEFINE WM505 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM505 DEFINE WP501 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP501 DEFINE WP503 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP503 DEFINE WP504 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP504 DEFINE WP505 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP505 DEFINE WP515 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP515 DEFINE WM503 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM503 DEFINE WP511 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP511 DEFINE WP512 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP512 DEFINE WP513 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP513 DEFINE WP514 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP514 DEFINE WP530 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP530 DEFINE WS505 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS505 DEFINE WT530 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT530 ;Calculates the work for area 500 F C500 = WC501+WM505+WP501+WP503+WP504+WP505+WP530+WS505+WT530 F M500 = WP515+WM503+WP511+WP512 F S500 = WP513+WP514 F WA500=C500+M500+S500 ; AREA 600 WORK STREAMS DEFINE WM604 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM604 DEFINE WP602 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP602 DEFINE WP606 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP606 DEFINE WS600 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS600 DEFINE WT602 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT602 DEFINE WT606 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT606 DEFINE WC614 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC614 DEFINE WM612 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM612 DEFINE WP608 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP608 DEFINE WP610 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP610 DEFINE WP611 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP611 DEFINE WP614 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP614 DEFINE WP616 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP616 DEFINE WS614 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS614 DEFINE WT608 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT608 DEFINE WT610 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT610 ;Calculates the work for area 600 F C600 = WM604+WP602+WP606 F M600 = WS600+WT602+WT606+WC614+WM612+WP608+WP610 F S600 = WP611+WP614+WP616+WS614+WT608+WT610 F WA600= C600+M600+S600 ; AREA 700 WORK STREAMS DEFINE WC755 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WC755 DEFINE WP701 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP701 DEFINE WP703 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP703 DEFINE WP704 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP704 DEFINE WP706 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP706 DEFINE WP707 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP707 DEFINE WP708 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP708 DEFINE WP710 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP710 DEFINE WP720 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP720 DEFINE WP750 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP750 DEFINE WP755 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP755 DEFINE WP760 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP760 DEFINE WT720 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT720 DEFINE WT760 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WT760 ;Calculates the work for area 700 F C700 = WP701+WP703+WP704+WT720+WT760 F M700 = WP706+WP707+WP708+WP755+WP760 F S700 = WP710+WP720+WP750+WC755 F WA700= C700+M700+S700 ; AREA 800 WORK STREAMS DEFINE WM801 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM801 DEFINE WM804 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM804 DEFINE WCOMB INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WCOMBFAN DEFINE WP811 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP811 DEFINE WP804 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP804 DEFINE WP824 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP824 DEFINE WP826 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP826 DEFINE WP828 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP828 DEFINE WP830 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP830 DEFINE WM830 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM830 DEFINE WM832 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM832 DEFINE WM834 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM834 DEFINE WPLNT INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WPLNTPOW ;Calculates the work for area 800 F C800 = WM801+WM804+WCOMB+WP811+WPLNT F M800 = WP804+WP824+WP826+WP828+WP830+WM830 F S800 = WM834+WM832 F WA800= C800+M800+S800 ; AREA 900 WORK STREAMS DEFINE WM902 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM902 DEFINE WM904A INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM904A DEFINE WM908 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM908 DEFINE WS904 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WS904 DEFINE WP912 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP912 DEFINE WP914 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP914 DEFINE WP902 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WP902 DEFINE WM910 INFO-VAR INFO=WORK VARIABLE=POWER STREAM=WM910 ;Calculates the work for area 900 F C900 = WM902+WM904A+WM908 F M900 = WS904+WP912 F S900 = WP914+WP902+WM910 F WA900= C900+M900+S900 ; DEFINE ZET502 MASS-FLOW STREAM=502 SUBSTREAM=MIXED COMPONENT=ETHANOL ; DEFINE ZA420 MASS-FLOW STREAM=420 SUBSTREAM=MIXED COMPONENT=ARABINOSE ; DEFINE ZET515 MASS-FLOW STREAM=515 SUBSTREAM=MIXED COMPONENT=ETHANOL ; ; ; Heat Exchangers ; H512 AREA DEFINE T501 STREAM-VAR STREAM=501 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T506 STREAM-VAR STREAM=506 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T518 STREAM-VAR STREAM=518 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T518A STREAM-VAR STREAM=518A SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX512 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH512 ; F DT512=((T501-T518A)-(T506-T518))/DLOG((T501-T518A)/(T506-T518)) F DT512 = dabs(DT512 * 1.8) F U512 = 200. C Convert from cal/s to BTU/hr F Q512 = QHX512 * 14.2869 C Area in square feet F A512 = DABS(Q512) / (U512 * DT512) ; ; H200 AREA DEFINE T221 STREAM-VAR STREAM=221 SUBSTREAM=MIXED VARIABLE=TEMP ; DEFINE T223L STREAM-VAR STREAM=223L SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T240 STREAM-VAR STREAM=240 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T945 STREAM-VAR STREAM=945 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T940 STREAM-VAR STREAM=940 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX200 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH200 F DT=((T221-T940)-(T240-T945))/DLOG((T221-T940)/(T240-T945)) F DT = DABS(DT * 1.8) F U = 250. C Convert from cal/s to BTU/hr F Q = QHX200 * 14.2869 C Area in square feet F A200 = DABS(Q) / (U * DT) F WRITE(NHSTRY,101)DT,Q,A200 F 101 FORMAT(' HX Calc Results',/, F 1 ' DT = ',g12.5,/, F 2 ' Q = ',g12.5,/, F 3 ' A200 = ',g12.5) ; ; H201 AREA DEFINE T218 STREAM-VAR STREAM=218 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T520A STREAM-VAR STREAM=520A SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T306 STREAM-VAR STREAM=306 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX201 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH201 ; DEFINE T222 STREAM-VAR STREAM=222 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QH201B INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH201B ; F DT1=((T218-T501)-(T222-T306))/DLOG((T218-T501)/(T222-T306)) F DT1 = DABS(DT * 1.8) F U = 150. C Convert from cal/s to BTU/hr F Q1 = QHX201 * 14.2869 ; F DT2=((T222-T501)-(T520A-T306))/DLOG((T222-T501)/(T520A-T306)) F DT2 = DABS(DT2 * 1.8) F U = 150. C Convert from cal/s to BTU/hr F Q2 = QH201B * 14.2869 ; C Area in square feet F A201A = DABS(Q1) / (U * DT1) F A201B = DABS(Q2) / (U * DT2) F A201 = A201A + A201B ; F WRITE(NHSTRY,102)DT1,Q1,DT2,Q2,A201 F 102 FORMAT(' HX Calc Results',/, F 1 ' DT1 = ',g12.5,/, F 2 ' Q1 = ',g12.5,/, F 3 ' DT2 = ',g12.5,/, F 4 ' Q2 = ',g12.5,/, F 5 ' A201 = ',g12.5) ; ; H205 AREA ;PneumaPress vent condenser ; DEFINE T260 STREAM-VAR STREAM=260 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T262 STREAM-VAR STREAM=262 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX205 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH205 ; F DT205=((T260-T940)-(T262-T945))/DLOG((T260-T940)/(T262-T945)) F DT205 = DABS(DT205 * 1.8) F U205 = 250. C Convert from cal/s to BTU/hr F Q205 = QHX205 * 14.2869 C Area in square feet F A205 = DABS(Q205) / (U205 * DT205) F WRITE(NHSTRY,101)DT205,Q205,A205 F 120 FORMAT(' HX Calc Results',/, F 1 ' DT205 = ',g12.5,/, F 2 ' Q205 = ',g12.5,/, F 3 ' A205 = ',g12.5) ; ; H244 AREA ; Based on H201 DEFINE T520 STREAM-VAR STREAM=520 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX244 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH244 F DT=((T520A-T940)-(T520-T945))/DLOG((T520A-T940)/(T520-T945)) F DT = DABS(DT * 1.8) F U = 150. C Convert from cal/s to BTU/hr F Q = QHX244 * 14.2869 C Area in square feet F A244 = DABS(Q) / (U * DT) F WRITE(NHSTRY,112)DT,Q,A244 F 112 FORMAT(' HX Calc Results',/, F 1 ' DT = ',g12.5,/, F 2 ' Q = ',g12.5,/, F 3 ' A244 = ',g12.5) ; ; H301 AREA ;HYDROLYZATE HEATER PRIOR TO SACCHARIFICATION ; U and specs for cost based on H512, plate and frame heat exchanger DEFINE T301 STREAM-VAR STREAM=301 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T301A STREAM-VAR STREAM=301A SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX301 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH301 F DT=((T301-T940)-(T301A-T945))/DLOG((T301-T940)/(T301A-T945)) F DT = DABS(DT * 1.8) F U = 200. C Convert from cal/s to BTU/hr F Q = QHX301 * 14.2869 C Area in square feet F A301 = DABS(Q) / (U * DT) F WRITE(NHSTRY,103)DT,Q,A301 F 103 FORMAT(' HX Calc Results',/, F 1 ' DT = ',g12.5,/, F 2 ' Q = ',g12.5,/, F 3 ' A301 = ',g12.5) ; ;H302 AREA ;SACCHARIFIED SLURRY COOLER AFTER SACCHARIFICATION DEFINE T301B STREAM-VAR STREAM=301B SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T301C STREAM-VAR STREAM=301C SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX302 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH302 F DT=((T301B-T940)-(T301C-T945))/DLOG((T301B-T940)/(T301C-T945)) F DT = DABS(DT * 1.8) F U = 300. C Convert from cal/s to BTU/hr F Q = QHX302 * 14.2869 C Area in square feet F A302 = DABS(Q) / (U * DT) F WRITE(NHSTRY,104)DT,Q,A302 F 104 FORMAT(' HX Calc Results',/, F 1 ' DT = ',g12.5,/, F 2 ' Q = ',g12.5,/, F 3 ' A302 = ',g12.5) ; ; H502 AREA DEFINE T526 STREAM-VAR STREAM=526 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T528 STREAM-VAR STREAM=528 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QEX502 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QE502A F DT = T526-T528 F DT = DABS(DT * 1.8) F U = 170. C Convert from cal/s to BTU/hr F Q = QEX502 * 14.2869 C Area in square feet F AE502 = DABS(Q) / (U * DT) F WRITE(NHSTRY,105)DT,Q,AE502 F 105 FORMAT(' HX Calc Results',/, F 1 ' DT = ',g12.5,/, F 2 ' Q = ',g12.5,/, F 3 ' AE502 = ',g12.5) C ; ; Use Diameter of 501 squared for scaling F DI501 = DD501 * DD501 ; DEFINE T612 STREAM-VAR STREAM=612 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T613 STREAM-VAR STREAM=613 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX602 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH602 F DT=((T612-T940)-(T613-T945))/DLOG((T612-T940)/(T613-T945)) F DT = DABS(DT * 1.8) F U = 115. C Convert from cal/s to BTU/hr F Q = QHX602 * 14.2869 C Area in square feet F A602 = DABS(Q) / (U * DT) F WRITE(NHSTRY,106)DT,Q,A602 F 106 FORMAT(' HX Calc Results',/, F 1 ' DT = ',g12.5,/, F 2 ' Q = ',g12.5,/, F 3 ' A602 = ',g12.5) ; ; H811 AREA DEFINE T812B STREAM-VAR STREAM=812B SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T823 STREAM-VAR STREAM=823 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T813A STREAM-VAR STREAM=813A SUBSTREAM=MIXED VARIABLE=TEMP DEFINE T813B STREAM-VAR STREAM=813B SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX811 INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH811 ; DEFINE T819 STREAM-VAR STREAM=819 SUBSTREAM=MIXED VARIABLE=TEMP DEFINE QHX81B INFO-VAR INFO=HEAT VARIABLE=DUTY STREAM=QH811B F DT1=((T812B-T813B)-(T819-T813A))/DLOG((T812B-T813B)/(T819-T813A)) F DT1 = DABS(DT1 * 1.8) F U = 700. C Convert from cal/s to BTU/hr F Q1 = QHX811 * 14.2869 ; ;F DT2=((T819-T813B)-(T823-T813A))/DLOG((T819-T813B)/(T823-T813A)) F DT2=T813B-T813A F DT2 = DABS(DT1 * 1.8) F U = 700. C Convert from cal/s to BTU/hr F Q2 = QHX81B * 14.2869 ; C Area in square feet F A811A = DABS(Q1) / (U * DT1) F A811B = DABS(Q2) / (U * DT2) F A811 = A811A + A811B ; F WRITE(NHSTRY,110)DT1,Q1,DT2,Q2,A811 F 110 FORMAT(' HX H-811 Calc Results',/, F 1 ' DT1 = ',g12.5,/, F 2 ' Q1 = ',g12.5,/, F 3 ' DT2 = ',g12.5,/, F 4 ' Q2 = ',g12.5,/, F 5 ' A811 = ',g12.5) ; ; WWT Volume Calculations ; THIS CODE CALCULATES THE SIZE OF THE ANAEROBIC DIGESTOR ; AND THE AEROBIC SYSTEM. ; DEFINE TOTANA STREAM-PROP STREAM=632 PROPERTY=MASSFLW DEFINE TOTAER STREAM-PROP STREAM=618 PROPERTY=MASSFLW DEFINE D618 STREAM-VAR STRM=618 SUBSTREAM=MIXED VAR=MASS-DENSITY C F ANLOAD = 12.0 F AELOAD = 0.55 C C ANLOAD AND AELOAD ARE THE SPACE LOADINGS IN G/L/D FOR THE ANAEROBIC C AND AEROBIC SYSTEMS, RESPECTIVELY C BOTH VALUES WERE PROVIDED BY J. RUOCCO C F ANCONC = (CODTOT*1000.)/TOTANA F AECONC = (COD2*1000.)/TOTAER C C ANCONC AND AECONC ARE THE COD CONCENTRATIONS (G/L) C THESE CALCULATIONS ASSUME THAT THE STREAMS HAVE THE SAME DENSITY C AS FOR WATER (1 KG/L). C F ANRT = (ANCONC*24.0)/ANLOAD F AERT = (AECONC*24.0)/AELOAD C C ANRT AND AERT ARE THE RESIDENCE TIME (H) FOR THE ANAEROBIC AND C AEROBIC SYSTEMS, RESPECTIVELY C F ANVOL1 = (TOTANA*ANRT)/3.7854 F AEVOL1 = (TOTAER*AERT)/3.7854 C C ANVOL AND AEVOL ARE THE VOLUMES (GAL) OF THE ANAEROBIC AND AEROBIC C SYSTEMS, RESPECTIVELY. C THIS CALCULATION ASSUMES THAT THE STREAMS HAVE THE SAME DENSITY AS C WATER (1 KG/L). C C Calculate the number of Anerobic Vessels, Assuming that the vessels C are limited to 962,651 gal. C F INMANR = INT (ANVOL1 / 962651.) + 1 F ANVOL = ANVOL1 / INMANR C C Second method of calculating Aerobic volume, 16.3 day residence time C Stream 618 is the inlet volume in Kg/hr C F AEVOL = TOTAER *2.2 * 24. * 16.3 / (8.33 * D618) F F WRITE(NHSTRY,108)TOTAER,D618,AEVOL F 108 FORMAT(' Total Flow to Aerobic: ',g12.5,' Kg/hr',/, F 1 ' Density of Stream 618: ',g12.5,' g/cc',/, F 2 ' Aerobic Volume, 15 day Res: ',g12.5,' gal') C F WRITE(NHSTRY,107)ANVOL1, INMANR, ANVOL, AEVOL1 F 107 FORMAT(' Total Anerobic Volume: ',g12.5,' gal',/, F 1 ' Number of Anerobic Tanks: ',i4,/, F 2 ' Volume of Each Anerobic Tank: ',g12.5,' gal',/, F 3 ' Total Aerobic Volume (Rucco): ',g12.5,' gal') C C Base Case of 4,569,250 Gal of Aerobic Lagoon, C Requires 16 Lagoon Aerators C or 285578 Gallons per Aerator F IWWTAG = AEVOL / 285578. + 1 F WRITE(NHSTRY,'('' Num of Aerators: '',g12.5)')IWWTAG ; ; Centrifuge Flow ; DEFINE F525M STREAM-VAR STRM=525 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE D525M STREAM-VAR STRM=525 SUBSTREAM=MIXED VAR=MASS-DENSITY DEFINE F525C STREAM-VAR STRM=525 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW DEFINE D525C STREAM-VAR STRM=525 SUBSTREAM=CISOLID VAR=MASS-DENSITY F D525A = (F525M*D525M + F525C*D525C)/(F525M + F525C) F GPM525 = (F525M + F525C) * 2.2 / (8.33 * D525A * 60.) C C Maximum flow to each centrifuge is 500 gpm C F NUMCNT = INT(GPM525/500.) + 1 F GPMCNT = GPM525 / NUMCNT C F WRITE(NHSTRY,109)D525A,GPM525,GPMCNT,NUMCNT F 109 FORMAT(' Stream 525 Density: ',g12.5,/, f 1 ' Stream 525 Flow: ',g12.5,' gpm',/, F 2 ' Flow to Each Centrifuge: ',g12.5,' gpm',/, F 3 ' Number of Centrifuges: ',i4) C ; Number of Reactors (Anco-Eaglin) ; DEFINE F217M STREAM-VAR STRM=217 SUBSTREAM=MIXED VARIABLE=MASS-FLOW DEFINE F217C STREAM-VAR STRM=217 SUBSTREAM=CISOLID VARIABLE=MASS-FLOW F F217 = F217M + F217C C C Original Anco-Eaglin quote for 3 reactors, $7,088,945 total purchased C Sized from 271,313 kg/hr (total flow stream 217) C Therefore, {271,313 kg/hr} / 3 reactors = 90437.67 kg/hr per reactor C F NUMRXN = INT(F217/90437.67) + 1 F RXNCNT = F217 / NUMRXN C F WRITE(NHSTRY,111)F217,RXNCNT,NUMRXN F 111 FORMAT(' Stream 217 Flow: ',g12.5,' kg/hr',/, F 2 ' Flow to Each Reactor: ',g12.5,' kg/hr',/, F 3 ' Number of Reactors: ',i4) C ; C DRYERS BEFORE BURNER NOT IN USE ; Number of Dryers ; (4050 kg/hr evaporated / per dryer from ReTec International Quote) ;F NUMDRY = INT(S851/4050.) + 1 ; ; Other Calculated Variables to be Tabulated ; F S51021 = S510 + S521 F S22156 = S221 + S256 ; C Heat duty to each Sacch. cooler F ISAC = SACVES F ISAC = ISAC + 1 F SACAGT = 2. * SACVES F ISACAG = 2 * ISAC F QH300A = QF300A / ISAC ; C Heat duty to each Ferm cooler F ISSF = SSFVES F ISSF = ISSF + 1 F SSFAGT = 2. * SSFVES F ISSFAG = 2 * ISSF F QEH300 = QF0300 / ISSF ; c Heat duty to each cellulase cooler (coils) F ICLVES = CLVES C 3 CELLULASE REACTORS NOT IN USE F ICLVES = ICLVES + 1 - 3 F QEH400 = QF0400 / ICLVES ;; TABULATE 1 AA220 COL-LABEL=ACET220A TABULATE 2 BODHP COL-LABEL=AEROBCHP TABULATE 3 COD2 COL-LABEL=AEROBCOD TABULATE 4 AEVOL COL-LABEL=AEROBVOL TABULATE 5 ANVOL COL-LABEL=ANEROVOL TABULATE 6 A200 COL-LABEL=AREA0200 TABULATE 7 A201 COL-LABEL=AREA0201 TABULATE 8 A205 COL-LABEL=AREA0205 TABULATE 9 A244 COL-LABEL=AREA0244 TABULATE 10 A301 COL-LABEL=AREA0301 TABULATE 11 A302 COL-LABEL=AREA0302 TABULATE 12 AE502 COL-LABEL=AREA0502 TABULATE 13 A512 COL-LABEL=AREA0512 TABULATE 14 A602 COL-LABEL=AREA0602 TABULATE 15 A811 COL-LABEL=AREA0811 TABULATE 16 HLETOT COL-LABEL=BURNLOHV TABULATE 17 GPMCNT COL-LABEL=CENTFLOW TABULATE 18 CLVES COL-LABEL=CLVESSEL TABULATE 19 DI501 COL-LABEL=DIAMD501 TABULATE 20 BTU101 COL-LABEL=HIHV0101 TABULATE 21 INMANR COL-LABEL=INUMANER TABULATE 22 IWWTAG COL-LABEL=INUMLAGT TABULATE 23 ISAC COL-LABEL=INUMSACC TABULATE 24 ISACAG COL-LABEL=INUMSACA TABULATE 25 ISSF COL-LABEL=INUMSSCF TABULATE 26 ISSFAG COL-LABEL=INUMSSFA TABULATE 27 NUMCNT COL-LABEL=NUMRCENT TABULATE 28 NUMRXN COL-LABEL=NUMRREAC TABULATE 29 P501GP COL-LABEL=P501FLOW TABULATE 30 PS0506 COL-LABEL=PSEU0506 TABULATE 31 PS0511 COL-LABEL=PSEU0511 TABULATE 36 QCWCAP COL-LABEL=QCWCAPIT TABULATE 37 QH300A COL-LABEL=QHX310EA TABULATE 47 QEH300 COL-LABEL=QHX300EA TABULATE 48 QEH400 COL-LABEL=QHX400EA TABULATE 53 RXNCNT COL-LABEL=REACFLOW TABULATE 54 S22156 COL-LABEL=S221S256 TABULATE 55 S51021 COL-LABEL=S510S521 TABULATE 61 SACAGT COL-LABEL=SACCAGTR TABULATE 62 SACVES COL-LABEL=SACVESSL TABULATE 63 SSFAGT COL-LABEL=SSCFAGTR TABULATE 64 SSFVES COL-LABEL=SSFVESSL TABULATE 65 WATCON COL-LABEL=WATRCONC TABULATE 100 WA100 COL-LABEL=WORKA100 TABULATE 102 WA200 COL-LABEL=WORKA200 TABULATE 103 WA300 COL-LABEL=WORKA300 TABULATE 104 WA400 COL-LABEL=WORKA400 TABULATE 105 WA500 COL-LABEL=WORKA500 TABULATE 106 WA600 COL-LABEL=WORKA600 TABULATE 107 WA700 COL-LABEL=WORKA700 TABULATE 108 WA900 COL-LABEL=WORKA900 TABULATE 109 WA800 COL-LABEL=WORKA800 ; Write Variable - Molecular weight of SOLSLDS, EXTRACT and PROTEIN DEFINE SOLMW UNARY-PARAM VARIABLE=MW ID1=SOLSLDS ID2=1 DEFINE EXTMW UNARY-PARAM VARIABLE=MW ID1=EXTRACT ID2=1 DEFINE PROMW UNARY-PARAM VARIABLE=MW ID1=PROTEIN ID2=1 TABULATE 110 SOLMW COL-LABEL=MOWTSOLS TABULATE 111 EXTMW COL-LABEL=MOWTEXTR TABULATE 112 PROMW COL-LABEL=MOWTPROT ; ; PARAM BASE-CASE=NO VARY STREAM-VAR STREAM=101 SUBSTREAM=MIXED & VARIABLE=TEMP LABEL="101 TEMP" RANGE LIST=20