Output file for simplified EB plant model
The following is the output file produced from running the EB plant model.The file is plain text and may viewed by any text browser, such as LIST or NOTEPAD, or by any word processor. It also may be printed directly from the PD-PLUS operating "shell."
Appearing first in the file is a formatted echo of what was in the input data file. Abbreviations in the input file are expanded and some description is added to make the report more readable. At the end of the input echo is a flowsheet connectivity summary and a list of the streams that will be recycle streams (called "tear streams" in some other simulators).
Following that is the calculation history, showing progress of control loops and recycles toward convergence. Any trace information and error messages produced for individual blocks also appear in the history. At the end of the history is the execution time, calculated as elapsed clock time less any time spent waiting in the interactive mode. This calculation time is of no particular use, except perhaps to embarrass other simulators. In the output file appearing below, the time shown (4.7 sec) was for execution on a 166 MHz Pentium PC. When the output file is printed from within the PD-PLUS operating shell, the calculation history normally is suppressed.
After the calculation history is the output report, consisting of a report for each block and then for each stream, followed by any heat curves requested. The lists and order of block and stream reports produced can be customized, if desired. Also, custom stream reports may be written to a separate file.
PD-PLUS CHEMICAL PROCESS SIMULATOR (c) Copyright 1988-2000, Deerhaven Technical Software - All Rights Reserved. Version 4.96 (Jan 2001). Serial 0000000. Deerhaven Technical Software.
DATA FILE: \XYZCHEM\EBPLANT1.dat APR 8, 2001 17:57:35
Simplified process for manufacture of ethylbenzene from ethylene
and benzene. Benzene and ethylene are reacted in a multi-bed,
vapor-phase alkylation reactor at high temperature. Part of the
ethylene and benzene are fed between reactor beds to absorb heat
of reaction and prevent overheating. Reactor effluent is used to
vaporize fresh and recycle benzene to the reactor.
In the first distillation, unreacted benzene is recovered and recycled to the reactor. Bottoms from the column is fed to the second column, where ethylbenzene product is recovered as distillate. The ethylbenezene column bottoms is fed to the third column, where diethylbenzene is recovered and recycled to the reactor for conversion to more ethylbenzene. The bottoms of third column is heavy residue.
COMPONENT DEFINITION
Retrieving from library: c:\dipprv11\dippr.db 1 Hydrogen LIBRARY NO. 1 2 Ethylene LIBRARY NO. 22 3 Ethane LIBRARY NO. 3 4 Benzene LIBRARY NO. 40 5 Toluene LIBRARY NO. 41 6 Ethylbenzene LIBRARY NO. 45 7 m/p-Xylene LIBRARY NO. 43 8 Cumene LIBRARY NO. 574 9 Diethylbenzenes LIBRARY NO. 611 10 Heavies LIBRARY NO. 666 11 Water LIBRARY NO. 51
K VALUE DATA SET 1
SOAVE VAPOR FUGACITY
SOAVE LIQUID FUGACITY
ENTHALPY DATA SET 1
SOAVE DEPARTURE FROM IDEAL GAS
MIXTURE PROPERTY CALCULATIONS
PROPERTIES TO BE CALCULATED USING DEFAULT METHODS
DEFAULT INPUT UNITS - TEMP=F, PRESS=PSIG, HEAT=BTU/HR, FLOW=LB/HR OUTPUT UNITS - TEMP=F, PRESS=PSIG, HEAT=BTU/HR, FLOW=LB/HR, LBMOL/HR
THE FOLLOWING STREAMS WILL BE PRINTED: 1 Fresh benzene to process 2 Cold ethylene feed 2A Hot ethylene to reactor 3 Fresh & recycle benzene from benzene column 3A Benzene from feed pump 3B Benzene from feed preheater 3C Benzene vapor from vaporizer 3D Benzene for reactor bed 1 to fired heater 3E Quench benzene for remaining reactor beds 3F Benzene for reactor bed 1 from fired heater 4 Hot reactor effluent 4A Reactor effluent from feed vaporizer 4B Reactor effluent from column reboiler 5 Benzene recovery column bottoms 5A Benzene column bottoms fed to EB column 6 Hot EB product from EB column 6A Cool EB product to tankage 7 EB recovery column bottoms 8 PEB column distillate 8A Recycle PEB from pump 8B Recycle PEB from heater 9 Process residue 10 Vent from benzene column
RECYCLE STREAM CONVERGENCE PARAMETERS
ACCELERATION DATA
CONVERGENCE TOLERANCES MAX. BOUNDS
STREAM RELATIVE ABSOLUTE TEMP ITER. LOWER UPPER FREQUENCY
(DEFAULTS) 0.00010 0.100 LB 0.1 F 100 -50.0 0.0 1
STREAM 1
TEMPERATURE= 250.0 F
PRESSURE= 250.00 PSIG
Benzene feed composition, flow calc by process
TOTAL FLOW= 10000.0 LB/HR
COMPONENT FLOWS:
0.00000 0.00000 0.00000 9950.0000 50.0000
COMPONENT FLOWS ADDED TO 100.00, HAVE BEEN SCALED TO SPECIFIED TOTAL.
STREAM 2
TEMPERATURE= 80.0 F
PRESSURE= 350.00 PSIG
ethylene feed composition
TOTAL FLOW= 3500.0 LB/HR
COMPONENT FLOWS:
0.00000 3493.0000 7.0000
COMPONENT FLOWS ADDED TO 1.00, HAVE BEEN SCALED TO SPECIFIED TOTAL.
STREAM CWS
TEMPERATURE= 85.0 F
PRESSURE= 60.000 PSIG
cooling water supply
TOTAL FLOW= 1000.0 LB/HR
COMPONENT FLOWS:
0.00000 0.00000 0.00000 0.00000 0.00000
0.00000 0.00000 0.00000 0.00000 0.00000
1000.0000
COMPONENT FLOWS ADDED TO 1.00, HAVE BEEN SCALED TO SPECIFIED TOTAL.
STREAM HPS
FRACTION LIQUID= 0.0000
PRESSURE= 600.00 PSIG
high pressure steam supply
TOTAL FLOW= 1000.0 LB/HR
COMPONENT FLOWS:
0.00000 0.00000 0.00000 0.00000 0.00000
0.00000 0.00000 0.00000 0.00000 0.00000
1000.0000
COMPONENT FLOWS ADDED TO 1.00, HAVE BEEN SCALED TO SPECIFIED TOTAL.
------------------------------------------------- Recycle stream estimates
STREAM 3C
TEMPERATURE= 500.0 F
PRESSURE= 315.00 PSIG
TOTAL FLOW= 200000.0 LB/HR
COMPONENT FLOWS:
0.00000 0.00000 0.00000 199800.0000 200.0000
COMPONENT FLOWS ADDED TO 1.00, HAVE BEEN SCALED TO SPECIFIED TOTAL.
STREAM 8A
TEMPERATURE= 100.0 F
PRESSURE= 300.00 PSIG
TOTAL FLOW= 1000.0 LB/HR
COMPONENT FLOWS:
0.00000 0.00000 0.00000 0.00000 0.00000
0.00000 0.00000 10.0000 989.0000 1.0000
COMPONENT FLOWS ADDED TO 1.00, HAVE BEEN SCALED TO SPECIFIED TOTAL.
HEAT EXCHANGER BLOCK E104C Ethylene feed heater, E-104, cold side
COLD STREAM 2
OUTLET STREAM 2A
TEMPERATURE = 250.0 F
PRESSURE DROP = 5.000 PSI
CALCULATOR BLOCK CALCBZ Calculate flow of benzene needed for reactor
1 ; Set benzene mass flow at 20 times that of feed ethylene
2 BZFLOW = STREAM 2A COMP 2 WT FLOW *20
3 STREAM 3C WT FLOW = BZFLOW ;poke flow into recycle benzene estimate.
4 NONOUTPUT 3C; setting flow does not close the recycle - tell PD-PLUS!
5 BLOCK C101 BZDIST = BZFLOW; also poke needed flow into column spec.
HEAT EXCHANGER BLOCK H101A Heat recycled PEB in heater
COLD STREAM 8A
OUTLET STREAM 8B
TEMPERATURE = 400.0 F
PRESSURE DROP = 20.000 PSI
SPLIT BLOCK BED1BZ Split off benzene for first reactor bed
FEED STREAMS: 3C
STREAM 3D FLOW= 0.750 OF TOTAL FEED
STREAM 3E FLOW IS INPUT MINUS OTHER OUTPUTS
HEAT EXCHANGER BLOCK H101B Heat bed 1 benzene in heater
COLD STREAM 3D
OUTLET STREAM 3F
TEMPERATURE = 810.0 F
PRESSURE DROP = 35.000 PSI
REACTOR BLOCK R101 Alkylation reactor, R-101
FEED STREAMS: 2A 3E 3F 8B
PRODUCT STREAM: 4
PRESSURE DROP= 50.000 PSI
CALCULATE HEAT OF REACTION
LEVEL 1 REACTIONS:
EQUATION 1 STOICHIOMETRY, MOL BASIS:
8 -1.000 6 1.000 2 0.500
CONVERT 5.0000 % OF COMPONENT 8
EQUATION 2 STOICHIOMETRY, MOL BASIS:
9 -1.000 4 -1.000 6 2.000
CONVERT 50.0000 % OF COMPONENT 9
LEVEL 2 REACTIONS:
EQUATION 3 STOICHIOMETRY, MOL BASIS:
2 -1.000 4 -1.000 6 1.000
CONVERT 88.3000 % OF COMPONENT 2
EQUATION 4 STOICHIOMETRY, MOL BASIS:
2 -1.000 4 -1.000 7 1.000
CONVERT 0.1000 % OF COMPONENT 2
EQUATION 5 STOICHIOMETRY, MOL BASIS:
2 -1.500 4 -1.000 8 1.000
CONVERT 0.4000 % OF COMPONENT 2
EQUATION 6 STOICHIOMETRY, MOL BASIS:
2 -2.000 4 -1.000 9 1.000
CONVERT 10.0000 % OF COMPONENT 2
EQUATION 7 STOICHIOMETRY, MOL BASIS:
2 -1.000 4 -2.000 10 1.000 1 1.000
CONVERT 1.0000 % OF COMPONENT 2
HEAT EXCHANGER BLOCK E101E102 Cool effluent in E-101 & E-102
HOT STREAM 4
OUTLET STREAM 4B
TEMPERATURE = 500.0 F
PRESSURE DROP = 10.000 PSI
FLASH BLOCK EFFLDP Check effluent dew point at column inlet pressure
FEED STREAMS: 4B
L/F=0.0000
PRESSURE DROP= 0.000 PSI
COLUMN BLOCK C101 Benzene recovery column, C-101
COLUMN HAS 45 THEORETICAL STAGES
FEED STREAM 4B , STAGE 20
FEED STREAM 1 , STAGE 44, VARIES
CIRCULATING REBOILER , INLET STREAM C101RBFD
FRACTION VAPORIZATION= 0.200, WT BASIS
BAFFLE SEPARATES BOTTOMS FROM REBOILER FEED
CONDENSER, LABEL QC
VAPOR DISTILLATE, STREAM 10 FLOW= 10.0 LBMOL/HR
LIQUID DISTILLATE, STREAM 3 FLOW= 70000.0 LB/HR , EST.MW= 78.
LABEL =BZDIST
BOTTOMS, STREAM 5
WT. FRACTION=0.010000, COMPONENT 6, STREAM 3
WT. FRACTION=0.001000, COMPONENT 4, STREAM 5
PRESSURE= 110.00 PSIG, STAGE 45
PRESSURE= 113.00 PSIG, STAGE 44
PRESSURE= 117.00 PSIG, STAGE 1
ESTIMATED TEMPERATURE = 320.0 F, STAGE 45
ESTIMATED TEMPERATURE = 470.0 F, STAGE 1
VAPOR FROM STAGE 44 EST.FLOW= 3500.0 LBMOL/HR
VAPOR FROM STAGE 20 EST.FLOW= 3500.0 LBMOL/HR
VAPOR FROM STAGE 19 EST.FLOW= 500.0 LBMOL/HR
TRACE CONVERGENCE AT LEVEL 0
VARIABLES:
1 SIDESTREAMS
2 HEATER/COOLERS
1 CIRCULATING REBOILER
1 VARIED FEEDS
SPECS:
5 ON INTERNAL OR PRODUCT FLOWS, TEMPERATURE, PURITY, RECOVERY, ETC.
PUMP BLOCK P101 Reactor feed pump, P-101
FEED STREAMS: 3
PRODUCT STREAM: 3A
DISCHARGE PRESSURE = 335.00 PSIG
EFFICIENCY = 68.0 %
HEAT EXCHANGER BLOCK E103 Reactor feed preheater, E-103
HOT STREAM HPS
OUTLET STREAM FLOW IS CALCULATED
L/F =1.00000
PRESSURE = 585.00 PSIG
COLD STREAM 3A
OUTLET STREAM 3B
TEMPERATURE = 430.0 F
PRESSURE DROP = 5.000 PSI
CALCULATOR BLOCK E101DUTY Set vaporizer duty by difference
1 ;Hot reactor effluent vaporizes benzene in E-101 and reboils the
2 ;benzene column (E-102); combined duty was calculated before to fixed
3 ;column feed temperature; get the heat available for vaporization and
4 ;superheating the benzene here, and replace the dummy duty value below
5 ;in block E101.
6 BLOCK E101 'Q-SPEC' = BLOCK E101E102 'Q-CALC' -BLOCK C101 Q1
HEAT EXCHANGER BLOCK E101 Reactor feed vaporizer, E-101
HOT STREAM 4
OUTLET STREAM 4A
PRESSURE DROP = 5.000 PSI
COLD STREAM 3B
OUTLET STREAM 3C
PRESSURE DROP = 10.000 PSI
DUTY = 999. BTU/HR
CALCULATE WEIGHTED MTD, 10 EQUAL DUTY SECTIONS
(duty replaced)
HEAT EXCHANGER BLOCK E102 Benzene column reboiler, E-102
HOT STREAM 4A
OUTLET STREAM 4B
TEMPERATURE = 500.0 F
PRESSURE DROP = 5.000 PSI
COLD STREAM C101RBFD
OUTLET STREAM
CALCULATE WEIGHTED MTD, 10 EQUAL DUTY SECTIONS
HEAT EXCHANGER BLOCK E104 Ethylene feed heater, E-104
HOT STREAM 5
OUTLET STREAM 5A
PRESSURE DROP = 2.000 PSI
COLD STREAM 2
OUTLET STREAM 2A
TEMPERATURE = 250.0 F
PRESSURE DROP = 5.000 PSI
COLUMN BLOCK C102 EB recovery column, C-102
COLUMN HAS 50 THEORETICAL STAGES
FEED STREAM 5A , STAGE 15
REBOILER
CONDENSER
VAPOR DISTILLATE FLOW= 0.0 LBMOL/HR
LIQUID DISTILLATE, STREAM 6 EST.FLOW= 110.0 LBMOL/HR
BOTTOMS, STREAM 7
WT. FRACTION=0.000100, COMPONENT 8, STREAM 6
WT. FRACTION=0.050000, COMPONENT 6, STREAM 7
PRESSURE= 5.000 PSIG, STAGE 50
PRESSURE= 7.000 PSIG, STAGE 49
PRESSURE= 12.000 PSIG, STAGE 1
ESTIMATED TEMPERATURE = 300.0 F, STAGE 50
ESTIMATED TEMPERATURE = 320.0 F, STAGE 15
ESTIMATED TEMPERATURE = 400.0 F, STAGE 1
VAPOR FROM STAGE 49 EST.FLOW= 400.0 LBMOL/HR
TRACE CONVERGENCE AT LEVEL 0
VARIABLES:
1 SIDESTREAMS
2 HEATER/COOLERS
SPECS:
3 ON INTERNAL OR PRODUCT FLOWS, TEMPERATURE, PURITY, RECOVERY, ETC.
(INCLUDES 1 FOR ZERO VAPOR DISTILLATE)
HEAT EXCHANGER BLOCK E105 EB product cooler, E-105
HOT STREAM 6
OUTLET STREAM 6A
TEMPERATURE = 105.0 F
PRESSURE DROP = 2.000 PSI
COLD STREAM CWS
OUTLET STREAM FLOW IS CALCULATED
TEMPERATURE = 105.0 F
COLUMN BLOCK C103 PEB recovery column, C-103
COLUMN HAS 10 THEORETICAL STAGES
FEED STREAM 7 , STAGE 6
REBOILER
CONDENSER
VAPOR DISTILLATE FLOW= 0.0 LBMOL/HR
LIQUID DISTILLATE, STREAM 8 EST.FLOW= 5.0 LBMOL/HR
BOTTOMS, STREAM 9
INTERNAL REFLUX RATIO= 5.00
WT. FRACTION=0.050000, COMPONENT 9, STREAM 9
PRESSURE= 5.000 PSIA, STAGE 10
PRESSURE= 6.000 PSIA, STAGE 9
PRESSURE= 7.000 PSIA, STAGE 1
ESTIMATED TEMPERATURE = 275.0 F, STAGE 10
ESTIMATED TEMPERATURE = 315.0 F, STAGE 3
ESTIMATED TEMPERATURE = 450.0 F, STAGE 1
TRACE CONVERGENCE AT LEVEL 0
VARIABLES:
1 SIDESTREAMS
2 HEATER/COOLERS
SPECS:
3 ON INTERNAL OR PRODUCT FLOWS, TEMPERATURE, PURITY, RECOVERY, ETC.
(INCLUDES 1 FOR ZERO VAPOR DISTILLATE)
PUMP BLOCK P102 PEB recycle pump, P-102
FEED STREAMS: 8
PRODUCT STREAM: 8A
DISCHARGE PRESSURE = 300.00 PSIG
EFFICIENCY = 50.0 %
CALCULATOR BLOCK SUMMARY Summary of process results
1 REPORT 1,(BLOCK E103 'Q-CALC'/1E6)
2 1 FORMAT(' Reactor benzene preheating (via HPS):',F7.2,' MMBTU/hr')
3 REPORT 2,(BLOCK H101B 'Q-CALC'/1E6)
4 2 FORMAT(' Fired heater: Benzene superheating: ',F7.2,' MMBTU/hr')
5 REPORT 3,(BLOCK H101A 'Q-CALC'/1E6)
6 3 FORMAT(' Recycle DEB vaporizing:',F7.2,' MMBTU/hr')
7 QR_C101= BLOCK C101 Q1/1.E6
8 QR_C102= BLOCK C102 Q1/1.E6
9 QR_C103= BLOCK C103 Q1/1.E6
10 REPORT 4,QR_C101
11 4 FORMAT(' Reboiler duties: Benzene column: ',F7.2,' MMBTU/hr')
12 REPORT 5,QR_C102
13 5 FORMAT(' EB column: ',F7.2,' MMBTU/hr')
14 REPORT 6,QR_C103
15 6 FORMAT(' PEB column: ',F7.2,' MMBTU/hr')
16 REPORT 7,(QR_C101 +QR_C102 +QR_C103)
17 7 FORMAT(' Total: ',F7.2,' MMBTU/hr')
18 REPORT 8,(ABS(BLOCK C101 QC/1.0E6))
19 8 FORMAT(' Benzene column steam generation: ',F7.2,' MMBTU/hr')
20 REPORT 9,(STREAM 6A COMP 6 WT FRACTION*100)
21 9 FORMAT(' EB product purity:',F6.2,' %')
22 REPORT 10,(STREAM 6A COMP 4 WT FRACTION*1E6)
23 10 FORMAT(' Benzene:',I6,' ppm(wt)')
24 REPORT 11,(STREAM 6A COMP 5 WT FRACTION*1E6)
25 11 FORMAT(' Toluene:',I6,' ppm(wt)')
26 REPORT 12,(STREAM 6A COMP 7 WT FRACTION*1E6)
27 12 FORMAT(' Xylenes:',I6,' ppm(wt)')
28 REPORT 13,(STREAM 6A COMP 8 WT FRACTION*1E6)
29 13 FORMAT(' Cumene: ',I6,' ppm(wt)')
HEATING/COOLING PROFILES REQUESTED:
STREAM 4
PRESSURE (PSIG ) 220.00
FLASH FROM STREAM CONDITIONS TO DEW POINT
TEMPERATURE INCREMENT = 10.0 F
FLOWSHEET SUMMARY/ STREAM CONNECTIONS:
OPERATION BLOCK ID INPUT STREAMS OUTPUT STREAMS Description
--------- -------- ----------------- ----------------- --------------
Heatexch E104C 2 2A Ethylene feed heater, E-104, cold side
Calculator CALCBZ Calculate flow of benzene needed for reactor
Heatexch H101A 8A 8B Heat recycled PEB in heater
Split BED1BZ 3C 3D 3E Split off benzene for first reactor bed
Heatexch H101B 3D 3F Heat bed 1 benzene in heater
Reactor R101 2A 3E 4 Alkylation reactor, R-101
3F 8B
Heatexch E101E102 4 4B Cool effluent in E-101 & E-102
Flash EFFLDP 4B Check effluent dew point at column inlet pressure
Column C101 4B 1 C101RBFD 3 Benzene recovery column, C-101
10 5
Pump P101 3 3A Reactor feed pump, P-101
Heatexch E103 HPS 3A 3B Reactor feed preheater, E-103
Calculator E101DUTY Set vaporizer duty by difference
Heatexch E101 4 3B 4A 3C Reactor feed vaporizer, E-101
Heatexch E102 4A C101RBFD 4B Benzene column reboiler, E-102
Heatexch E104 5 2 5A 2A Ethylene feed heater, E-104
Column C102 5A 6 7 EB recovery column, C-102
Heatexch E105 6 CWS 6A EB product cooler, E-105
Column C103 7 8 9 PEB recovery column, C-103
Pump P102 8 8A PEB recycle pump, P-102
Calculator SUMMARY Summary of process results
WARNING: STREAM 4B IS AN OUTPUT MORE THAN ONCE IN THE SEQUENCE
WARNING: STREAM 2A IS AN OUTPUT MORE THAN ONCE IN THE SEQUENCE
FINAL RECYCLE LIST FOR THE DEFINED EXECUTION SEQUENCE:
8A 3C
--CALCULATION HISTORY--
AVG.FR.ERROR= 0.835E+00, 12 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR=102.30 F
AVG.FR.ERROR= 0.161E+00, 8 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 7.38 F
AVG.FR.ERROR= 0.198E+00, 6 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 12.45 F
AVG.FR.ERROR= 0.242E-01, 3 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 0.31 F
AVG.FR.ERROR= 0.156E-02, 2 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 0.00 F
AVG.FR.ERROR= 0.578E-03, 1 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 0.00 F
AVG.FR.ERROR= 0.209E-03, 1 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 0.00 F
AVG.FR.ERROR= 0.144E-02, 1 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 0.01 F
AVG.FR.ERROR= 0.586E-03, 0 NOT CONVERGED, RECYCLES 8A 3C
AVG. TEMP. ERROR= 0.00 F
SOLUTION TIME= 0 MIN., 4.7 SEC.
--OUTPUT REPORT--
HEAT EXCHANGER BLOCK E104C Ethylene feed heater, E-104, cold side
DUTY= 0.2723 MM BTU/HR
COLD SIDE INLET TEMP= 80.0 F, L/F=0.0000, FLOW= 3500.00 LB/HR
VAPOR DENSITY= 2.091 LB/FT3
OUTLET TEMP= 250.0 F, L/F=0.0000
VAPOR DENSITY= 1.400 LB/FT3
HEAT EXCHANGER BLOCK H101A Heat recycled PEB in heater
DUTY= 0.1895 MM BTU/HR
COLD SIDE INLET TEMP= 264.2 F, L/F=1.0000, FLOW= 2566.34 LB/HR
LIQUID DENSITY= 48.09 LB/FT3
OUTLET TEMP= 400.0 F, L/F=1.0000
LIQUID DENSITY= 43.48 LB/FT3
HEAT EXCHANGER BLOCK H101B Heat bed 1 benzene in heater
DUTY= 10.1093 MM BTU/HR
COLD SIDE INLET TEMP= 448.0 F, L/F=0.0254, FLOW= 52395.30 LB/HR
OUTLET TEMP= 810.0 F, L/F=0.0000
VAPOR DENSITY= 1.840 LB/FT3
REACTOR BLOCK R101 Alkylation reactor, R-101
PRODUCT TEMPERATURE = 811.1 F
PRESSURE = 230.00 PSIG
L/F =0.0000
HEAT ADDED = 0.0 BTU/HR
COMPONENT CHANGES, LBMOL/HR:
1 +1.25 2 -124.46 4 -125.62 6 +122.89
7 +0.12 8 +0.01 9 +0.09 10 +1.25
HEAT EXCHANGER BLOCK E101E102 Cool effluent in E-101 & E-102
DUTY= 12.4200 MM BTU/HR
HOT SIDE INLET TEMP= 811.1 F, L/F=0.0000, FLOW= 75926.64 LB/HR
VAPOR DENSITY= 1.586 LB/FT3
OUTLET TEMP= 500.0 F, L/F=0.0000
VAPOR DENSITY= 2.287 LB/FT3
FLASH BLOCK EFFLDP Check effluent dew point at column inlet pressure
TEMPERATURE= 445.3 F, PRESSURE= 220.00 PSIG
MOL FRACTION LIQUID=0.00000
HEAT REMOVED= 2.013 MM BTU/HR
K VALUES:
36.429 11.000 9.4737 1.2707 0.83128
0.57118 0.55385 0.44576 0.28048 0.45640E-01
9.7681
WARNING: VAPOR OR LIQUID EXISTS BUT WAS NOT SAVED AS A STREAM
COLUMN BLOCK C101 Benzene recovery column, C-101
COLUMN SUMMARY. FLOWS ARE IN LBMOL/HR
STAGE TEMP PRESS FLOW FROM STAGE FEED PRODUCT HEAT ADDED
F PSIG VAPOR LIQUID MM BTU/HR
45 320.5 110.00 700.8 10.0 VAP -18.659
893.2 LIQ
44 341.6 113.00 1604.1 924.2 134.8
43 343.8 113.09 1692.6 911.5
42 346.9 113.19 1680.0 894.2
41 351.0 113.28 1662.6 873.5
40 356.0 113.37 1642.0 852.2
39 361.6 113.47 1620.6 833.0
38 367.0 113.56 1601.4 817.8
37 371.7 113.65 1586.2 807.0
36 375.5 113.74 1575.4 799.7
35 378.3 113.84 1568.1 795.1
34 380.2 113.93 1563.5 792.1
33 381.6 114.02 1560.6 790.3
32 382.5 114.12 1558.7 789.1
31 383.1 114.21 1557.5 788.4
30 383.6 114.30 1556.8 787.9
29 383.9 114.40 1556.3 787.5
28 384.1 114.49 1556.0 787.3
27 384.3 114.58 1555.7 787.0
26 384.5 114.67 1555.4 786.7
25 384.6 114.77 1555.1 786.2
24 384.8 114.86 1554.6 785.4
23 385.1 114.95 1553.8 783.9
22 385.5 115.05 1552.3 780.7
21 386.3 115.14 1549.1 772.9
20 388.1 115.23 1541.3 483.1 913.6
19 389.0 115.33 337.9 483.4
18 390.1 115.42 338.2 483.0
17 391.8 115.51 337.8 482.3
16 394.5 115.60 337.1 481.2
15 398.7 115.70 336.0 479.9
14 404.8 115.79 334.8 479.0
13 413.1 115.88 333.8 479.3
12 423.0 115.98 334.1 481.8
11 433.6 116.07 336.6 486.7
10 443.4 116.16 341.5 493.3
9 451.5 116.26 348.1 500.2
8 457.7 116.35 355.0 506.3
7 462.0 116.44 361.1 511.0
6 465.0 116.53 365.8 514.3
5 467.0 116.63 369.1 516.5
4 468.4 116.72 371.3 517.7
3 469.7 116.81 372.5 517.7
2 471.4 116.91 372.5 514.8
REB 475.1 117.00 369.6 1452.1 4.537
REBF 474.1 1821.7 RF
BTMS 475.1 145.2 LIQ
FEED STREAM 4B TO STAGE 20 = 913.6 LBMOL/HR FEED STREAM 1 TO STAGE 44 = 134.8 LBMOL/HR LIQUID STREAM 3 FROM STAGE 45 = 893.2 LBMOL/HR VAPOR STREAM 10 FROM STAGE 45 = 10.0 LBMOL/HR BOTTOMS STREAM 5 = 145.2 LBMOL/HR FLOW TO REBOILER = 1821.7 LBMOL/HR AT 474.1 F, STREAM C101RBFD BOTTOMS IS DRAWN FROM REBOILER OUTLET SIDE OF BAFFLE EXTERNAL REFLUX RATIO= 0.776 INTERNAL REFLUX RATIO= 1.023
--------------VAPOR------------- --------------LIQUID-------------
WT FLOW MW VOL FLOW DENSITY WT FLOW MW VOL FLOW DENSITY
STAGE LB/HR FT3/SEC LB/FT3 LB/HR GPM LB/FT3
45 673.2 67.3 0.17 1.1195 54809.4 78.2 152.86 44.7
44 125342.5 78.1 25.74 1.3526 72807.7 78.8 207.41 43.8
43 132801.2 78.5 27.21 1.3556 72447.3 79.5 206.74 43.7
42 132440.9 78.8 27.10 1.3577 71958.4 80.5 205.82 43.6
41 131951.9 79.4 26.94 1.3606 71452.8 81.8 205.00 43.5
40 131446.3 80.1 26.75 1.3647 71042.8 83.4 204.58 43.3
39 131036.3 80.9 26.57 1.3701 70815.5 85.0 204.74 43.1
38 130809.0 81.7 26.40 1.3764 70778.3 86.5 205.42 43.0
37 130771.7 82.4 26.27 1.3828 70869.8 87.8 206.38 42.8
36 130863.3 83.1 26.18 1.3887 71014.8 88.8 207.35 42.7
35 131008.2 83.5 26.11 1.3936 71159.0 89.5 208.19 42.6
34 131152.4 83.9 26.07 1.3975 71278.4 90.0 208.83 42.6
33 131271.6 84.1 26.04 1.4005 71367.0 90.3 209.30 42.5
32 131360.1 84.3 26.01 1.4029 71428.7 90.5 209.62 42.5
31 131422.2 84.4 25.99 1.4048 71469.9 90.7 209.84 42.5
30 131463.3 84.4 25.96 1.4064 71496.3 90.7 209.99 42.5
29 131489.6 84.5 25.94 1.4079 71512.6 90.8 210.09 42.4
28 131506.1 84.5 25.92 1.4091 71521.4 90.8 210.16 42.4
27 131514.8 84.5 25.90 1.4103 71524.2 90.9 210.20 42.4
26 131517.6 84.6 25.88 1.4115 71521.2 90.9 210.22 42.4
25 131514.6 84.6 25.86 1.4126 71509.0 91.0 210.22 42.4
24 131502.2 84.6 25.84 1.4137 71479.5 91.0 210.17 42.4
23 131472.9 84.6 25.81 1.4147 71412.7 91.1 210.02 42.4
22 131406.0 84.7 25.78 1.4157 71259.6 91.3 209.64 42.4
21 131253.1 84.7 25.74 1.4165 70822.2 91.6 208.46 42.4
20 130815.8 84.9 25.66 1.4162 44702.6 92.5 131.60 42.4
19 28769.4 85.1 5.62 1.4215 44798.8 92.7 131.98 42.3
18 28865.6 85.3 5.63 1.4245 44870.5 92.9 132.29 42.3
17 28937.2 85.7 5.63 1.4286 44985.5 93.3 132.80 42.2
16 29052.3 86.2 5.62 1.4348 45180.0 93.9 133.63 42.2
15 29246.7 87.0 5.62 1.4445 45510.3 94.8 135.02 42.0
14 29577.1 88.4 5.63 1.4595 46056.7 96.2 137.26 41.8
13 30123.5 90.2 5.65 1.4818 46902.5 97.9 140.65 41.6
12 30969.2 92.7 5.69 1.5123 48081.8 99.8 145.28 41.3
11 32148.5 95.5 5.76 1.5493 49520.8 101.7 150.87 40.9
10 33587.4 98.3 5.87 1.5884 51039.2 103.5 156.73 40.6
9 35106.1 100.8 6.00 1.6243 52434.6 104.8 162.10 40.3
8 36501.5 102.8 6.13 1.6538 53573.6 105.8 166.49 40.1
7 37640.4 104.2 6.24 1.6760 54423.4 106.5 169.76 40.0
6 38490.1 105.2 6.32 1.6918 55019.6 107.0 172.06 39.9
5 39086.4 105.9 6.38 1.7029 55421.7 107.3 173.62 39.8
4 39488.5 106.3 6.41 1.7109 55683.8 107.6 174.67 39.7
3 39750.6 106.7 6.43 1.7170 55833.9 107.9 175.32 39.7
2 39900.7 107.1 6.43 1.7226 55774.4 108.3 175.32 39.7
REB 39841.2 107.8 6.40 1.7280 159364.8 109.7 501.09 39.7
REBF 199206.0 109.4 626.32 39.7
BTMS 15933.2 109.7 50.10 39.7
--------VAPOR--------- --------------LIQUID------------------
VISCOSITY THERM.COND. VISCOSITY THERM.COND. SURF.TENSION
STAGE CENTIPOISE BTU/FT-HR-F CENTIPOISE BTU/FT-HR-F DYNE/CM
45 0.01158 0.01697 0.153 0.05872 11.60
44 0.01175 0.01407 0.142 0.05673 10.39
43 0.01176 0.01412 0.142 0.05644 10.35
42 0.01177 0.01422 0.142 0.05603 10.29
41 0.01179 0.01434 0.141 0.05549 10.21
40 0.01181 0.01450 0.141 0.05485 10.10
39 0.01182 0.01467 0.141 0.05418 9.97
38 0.01184 0.01484 0.141 0.05356 9.84
37 0.01185 0.01499 0.141 0.05304 9.72
36 0.01185 0.01511 0.140 0.05264 9.62
35 0.01186 0.01519 0.140 0.05235 9.54
34 0.01186 0.01526 0.140 0.05214 9.49
33 0.01186 0.01530 0.140 0.05200 9.45
32 0.01186 0.01533 0.140 0.05191 9.42
31 0.01186 0.01535 0.140 0.05185 9.40
30 0.01186 0.01536 0.140 0.05180 9.39
29 0.01187 0.01537 0.140 0.05177 9.38
28 0.01187 0.01538 0.140 0.05175 9.37
27 0.01187 0.01539 0.140 0.05173 9.36
26 0.01187 0.01539 0.140 0.05172 9.35
25 0.01187 0.01540 0.140 0.05170 9.35
24 0.01187 0.01540 0.140 0.05169 9.34
23 0.01188 0.01541 0.140 0.05166 9.33
22 0.01188 0.01542 0.140 0.05163 9.32
21 0.01189 0.01544 0.140 0.05157 9.31
20 0.01190 0.01548 0.140 0.05148 9.30
19 0.01190 0.01547 0.140 0.05140 9.27
18 0.01190 0.01551 0.140 0.05130 9.23
17 0.01190 0.01556 0.140 0.05114 9.18
16 0.01190 0.01565 0.140 0.05088 9.10
15 0.01190 0.01579 0.140 0.05049 8.98
14 0.01189 0.01599 0.139 0.04992 8.79
13 0.01187 0.01627 0.139 0.04919 8.54
12 0.01184 0.01661 0.139 0.04833 8.23
11 0.01179 0.01698 0.139 0.04746 7.90
10 0.01174 0.01734 0.139 0.04666 7.59
9 0.01169 0.01763 0.140 0.04602 7.33
8 0.01165 0.01786 0.140 0.04554 7.14
7 0.01162 0.01803 0.140 0.04521 7.00
6 0.01160 0.01814 0.140 0.04498 6.91
5 0.01159 0.01821 0.141 0.04483 6.85
4 0.01158 0.01826 0.141 0.04473 6.81
3 0.01157 0.01830 0.141 0.04464 6.77
2 0.01157 0.01834 0.141 0.04456 6.73
REB 0.01158 0.01841 0.141 0.04447 6.69
REBF 0.141 0.04450 6.70
BTMS 0.141 0.04447 6.69
PUMP BLOCK P101 Reactor feed pump, P-101
HORSEPOWER = 37.6 AT 68.0 % EFFICIENCY
DRIVER POWER = 28.0 KILOWATT AT 100% EFFICIENCY
FLOW= 194.89 GAL/MIN, SPECIFIC GRAVITY= 0.7168
SUCTION PRESSURE= 110.00 PSIG, DISCHARGE PRESSURE= 335.00 PSIG
DISCHARGE TEMPERATURE= 323.0 F
HEAT EXCHANGER BLOCK E103 Reactor feed preheater, E-103
DUTY= 4.4204 MM BTU/HR
HOT SIDE INLET TEMP= 488.9 F, L/F=0.0000, FLOW= 6043.48 LB/HR
VAPOR DENSITY= 1.274 LB/FT3
OUTLET TEMP= 486.2 F, L/F=1.0000
LIQUID DENSITY= 49.76 LB/FT3
COLD SIDE INLET TEMP= 323.0 F, L/F=1.0000, FLOW= 69859.95 LB/HR
LIQUID DENSITY= 44.58 LB/FT3
OUTLET TEMP= 430.0 F, L/F=1.0000
LIQUID DENSITY= 38.72 LB/FT3
LMTD= 102.3 F, UNCORRECTED
MTD CORRECTION FACTOR (OVERALL, FOR EVEN TUBE PASS SHELLS):
0.995 FOR 1 SHELL
0.999 FOR 2 SHELLS
REQUIRED U*A= 43211.5 BTU/HR -F, BASED ON UNCORRECTED MTD
HEAT EXCHANGER BLOCK E101 Reactor feed vaporizer, E-101
DUTY= 7.8830 MM BTU/HR
HOT SIDE INLET TEMP= 811.1 F, L/F=0.0000, FLOW= 75926.64 LB/HR
VAPOR DENSITY= 1.586 LB/FT3
OUTLET TEMP= 619.2 F, L/F=0.0000
VAPOR DENSITY= 1.938 LB/FT3
COLD SIDE INLET TEMP= 430.0 F, L/F=1.0000, FLOW= 69859.95 LB/HR
LIQUID DENSITY= 38.72 LB/FT3
OUTLET TEMP= 448.0 F, L/F=0.0232
WT FRACTION VAPOR= 0.9766
VAPOR DENSITY= 3.802 LB/FT3
LIQUID DENSITY= 37.61 LB/FT3
MTD CORRECTION FACTOR (OVERALL, FOR EVEN TUBE PASS SHELLS):
0.992 FOR 1 SHELL
0.998 FOR 2 SHELLS
PROFILES (DEG F, FOR EQUAL DUTY SECTIONS):
HOT TEMP 811.1 792.7 774.1 755.3 736.4 717.3 698.0 678.6 659.0 639.2 619.2
L/F 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
COLD TEMP 448.0 448.2 448.4 448.6 448.7 448.9 448.9 448.8 448.3 445.9 430.0
L/F 0.0232 0.1325 0.2423 0.3523 0.4627 0.5731 0.6835 0.7933 0.9006 0.9958 1.0000
TEMP DIFF 363.1 344.5 325.7 306.7 287.7 268.4 249.1 229.8 210.7 193.3 189.2
WEIGHTED MTD= 258.3 F (UNCORRECTED)
REQUIRED U*A= 30514.3 BTU/HR -F, BASED ON UNCORRECTED MTD
HEAT EXCHANGER BLOCK E102 Benzene column reboiler, E-102
DUTY= 4.5370 MM BTU/HR
HOT SIDE INLET TEMP= 619.2 F, L/F=0.0000, FLOW= 75926.64 LB/HR
VAPOR DENSITY= 1.938 LB/FT3
OUTLET TEMP= 500.0 F, L/F=0.0000
VAPOR DENSITY= 2.287 LB/FT3
COLD SIDE INLET TEMP= 474.1 F, L/F=1.0000, FLOW= 199206.00 LB/HR
LIQUID DENSITY= 39.66 LB/FT3
OUTLET TEMP= 475.1 F, L/F=0.7971
WT FRACTION VAPOR= 0.2000
VAPOR DENSITY= 1.728 LB/FT3
LIQUID DENSITY= 39.65 LB/FT3
MTD CORRECTION FACTOR (OVERALL, FOR EVEN TUBE PASS SHELLS):
0.995 FOR 1 SHELL
0.999 FOR 2 SHELLS
PROFILES (DEG F, FOR EQUAL DUTY SECTIONS):
HOT TEMP 619.2 607.6 595.9 584.2 572.4 560.5 548.5 536.5 524.4 512.2 500.0
L/F 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000 0.0000
COLD TEMP 475.1 475.0 474.9 474.8 474.7 474.6 474.5 474.4 474.3 474.2 474.1
L/F 0.7971 0.8174 0.8376 0.8579 0.8781 0.8984 0.9187 0.9391 0.9594 0.9797 1.0000
TEMP DIFF 144.1 132.6 121.0 109.4 97.7 85.9 74.0 62.1 50.1 38.0 25.9
WEIGHTED MTD= 69.4 F (UNCORRECTED)
REQUIRED U*A= 65342.9 BTU/HR -F, BASED ON UNCORRECTED MTD
HEAT EXCHANGER BLOCK E104 Ethylene feed heater, E-104
DUTY= 0.2723 MM BTU/HR
HOT SIDE INLET TEMP= 475.1 F, L/F=1.0000, FLOW= 15933.20 LB/HR
LIQUID DENSITY= 39.65 LB/FT3
OUTLET TEMP= 448.2 F, L/F=1.0000
LIQUID DENSITY= 40.92 LB/FT3
COLD SIDE INLET TEMP= 80.0 F, L/F=0.0000, FLOW= 3500.00 LB/HR
VAPOR DENSITY= 2.091 LB/FT3
OUTLET TEMP= 250.0 F, L/F=0.0000
VAPOR DENSITY= 1.400 LB/FT3
LMTD= 290.8 F, UNCORRECTED
MTD CORRECTION FACTOR (OVERALL, FOR EVEN TUBE PASS SHELLS):
0.991 FOR 1 SHELL
0.998 FOR 2 SHELLS
REQUIRED U*A= 936.1 BTU/HR -F, BASED ON UNCORRECTED MTD
COLUMN BLOCK C102 EB recovery column, C-102
COLUMN SUMMARY. FLOWS ARE IN LBMOL/HR
STAGE TEMP PRESS FLOW FROM STAGE FEED PRODUCT HEAT ADDED
F PSIG VAPOR LIQUID MM BTU/HR
50 297.0 5.000 0.0 481.5 123.8 LIQ -9.433
49 304.3 7.000 605.2 493.4
48 304.8 7.104 617.2 493.5
47 305.2 7.208 617.3 493.6
46 305.5 7.313 617.4 493.7
45 305.9 7.417 617.4 493.7
44 306.2 7.521 617.5 493.8
43 306.6 7.625 617.6 493.8
42 306.9 7.729 617.6 493.9
41 307.3 7.833 617.7 494.0
40 307.6 7.938 617.7 494.0
39 307.9 8.042 617.8 494.1
38 308.3 8.146 617.8 494.1
37 308.6 8.250 617.9 494.2
36 309.0 8.354 618.0 494.2
35 309.3 8.458 618.0 494.3
34 309.7 8.563 618.0 494.3
33 310.0 8.667 618.1 494.4
32 310.3 8.771 618.1 494.4
31 310.7 8.875 618.2 494.4
30 311.0 8.979 618.2 494.5
29 311.4 9.083 618.2 494.5
28 311.7 9.188 618.3 494.5
27 312.1 9.292 618.3 494.5
26 312.5 9.396 618.3 494.5
25 312.9 9.500 618.3 494.5
24 313.2 9.604 618.3 494.5
23 313.6 9.708 618.2 494.4
22 314.0 9.813 618.2 494.4
21 314.5 9.917 618.1 494.3
20 314.9 10.021 618.0 494.1
19 315.4 10.125 617.9 493.8
18 315.9 10.229 617.6 493.4
17 316.6 10.333 617.2 492.5
16 317.6 10.438 616.2 490.3
15 319.3 10.542 614.0 558.3 145.2
14 319.9 10.646 536.9 558.1
13 320.7 10.750 536.7 557.7
12 321.6 10.854 536.3 557.2
11 322.8 10.958 535.8 556.3
10 324.3 11.063 534.9 555.2
9 326.1 11.167 533.8 553.6
8 328.5 11.271 532.2 551.6
7 331.4 11.375 530.2 548.8
6 335.1 11.479 527.4 544.9
5 339.9 11.583 523.5 539.2
4 346.4 11.688 517.8 531.3
3 355.2 11.792 509.9 521.8
2 366.3 11.896 500.4 506.7
1 382.1 12.000 485.3 21.4 LIQ 8.187
FEED STREAM 5A TO STAGE 15 = 145.2 LBMOL/HR LIQUID STREAM 6 FROM STAGE 50 = 123.8 LBMOL/HR BOTTOMS STREAM 7 = 21.4 LBMOL/HR EXTERNAL REFLUX RATIO= 3.890 INTERNAL REFLUX RATIO= 3.986
--------------VAPOR------------- --------------LIQUID-------------
WT FLOW MW VOL FLOW DENSITY WT FLOW MW VOL FLOW DENSITY
STAGE LB/HR FT3/SEC LB/FT3 LB/HR GPM LB/FT3
50 0.0 105.9 0.00 0.2685 51064.6 106.1 135.98 46.8
49 64191.9 106.1 60.54 0.2945 52361.1 106.1 140.23 46.6
48 65488.5 106.1 61.46 0.2960 52384.2 106.1 140.34 46.5
47 65511.4 106.1 61.20 0.2973 52396.1 106.2 140.41 46.5
46 65523.4 106.1 60.94 0.2987 52404.9 106.2 140.48 46.5
45 65532.2 106.1 60.67 0.3000 52412.4 106.2 140.53 46.5
44 65539.8 106.1 60.41 0.3014 52419.6 106.2 140.59 46.5
43 65546.8 106.1 60.15 0.3027 52426.6 106.2 140.65 46.5
42 65553.8 106.1 59.89 0.3040 52433.7 106.2 140.71 46.5
41 65561.0 106.1 59.64 0.3054 52441.0 106.2 140.76 46.4
40 65568.2 106.1 59.39 0.3067 52448.2 106.2 140.82 46.4
39 65575.3 106.1 59.13 0.3080 52455.7 106.2 140.88 46.4
38 65583.0 106.1 58.89 0.3094 52463.2 106.2 140.94 46.4
37 65590.4 106.2 58.64 0.3107 52471.0 106.2 141.00 46.4
36 65598.1 106.2 58.39 0.3120 52478.7 106.2 141.06 46.4
35 65606.1 106.2 58.15 0.3134 52486.8 106.2 141.12 46.4
34 65614.2 106.2 57.91 0.3147 52495.2 106.2 141.18 46.4
33 65622.6 106.2 57.67 0.3161 52504.2 106.2 141.24 46.3
32 65631.5 106.2 57.44 0.3174 52513.1 106.2 141.31 46.3
31 65640.4 106.2 57.20 0.3188 52522.8 106.2 141.37 46.3
30 65650.0 106.2 56.97 0.3201 52532.7 106.2 141.44 46.3
29 65660.0 106.2 56.74 0.3215 52543.2 106.3 141.51 46.3
28 65670.5 106.2 56.51 0.3228 52554.3 106.3 141.58 46.3
27 65681.6 106.2 56.28 0.3242 52566.0 106.3 141.65 46.3
26 65693.3 106.3 56.05 0.3255 52578.4 106.3 141.73 46.3
25 65705.7 106.3 55.83 0.3269 52591.8 106.4 141.81 46.2
24 65719.0 106.3 55.61 0.3283 52606.3 106.4 141.90 46.2
23 65733.6 106.3 55.38 0.3297 52622.0 106.4 141.98 46.2
22 65749.3 106.4 55.16 0.3311 52639.1 106.5 142.08 46.2
21 65766.4 106.4 54.94 0.3325 52657.3 106.5 142.18 46.2
20 65784.6 106.4 54.72 0.3339 52676.2 106.6 142.28 46.2
19 65803.5 106.5 54.51 0.3354 52693.8 106.7 142.39 46.1
18 65821.1 106.6 54.28 0.3368 52706.7 106.8 142.49 46.1
17 65834.0 106.7 54.05 0.3383 52704.3 107.0 142.56 46.1
16 65831.5 106.8 53.81 0.3399 52635.8 107.4 142.48 46.1
15 65763.1 107.1 53.50 0.3414 60378.5 108.2 163.53 46.0
14 57572.6 107.2 46.61 0.3431 60456.2 108.3 163.84 46.0
13 57650.2 107.4 46.44 0.3448 60549.8 108.6 164.20 46.0
12 57743.8 107.7 46.27 0.3467 60668.6 108.9 164.66 45.9
11 57862.6 108.0 46.09 0.3487 60823.0 109.3 165.25 45.9
10 58016.9 108.5 45.90 0.3511 61023.6 109.9 166.01 45.8
9 58217.5 109.1 45.71 0.3538 61279.1 110.7 166.97 45.8
8 58473.1 109.9 45.51 0.3569 61593.0 111.7 168.17 45.7
7 58787.0 110.9 45.30 0.3605 61956.1 112.9 169.57 45.6
6 59150.0 112.1 45.07 0.3645 62342.4 114.4 171.12 45.4
5 59535.8 113.7 44.80 0.3691 62716.2 116.3 172.75 45.3
4 59909.9 115.7 44.47 0.3743 63081.4 118.7 174.49 45.1
3 60275.3 118.2 44.05 0.3801 63505.8 121.7 176.55 44.8
2 60699.8 121.3 43.60 0.3867 63443.2 125.2 177.26 44.6
1 60637.1 124.9 42.90 0.3926 2805.9 131.1 7.81 44.8
--------VAPOR--------- --------------LIQUID------------------
VISCOSITY THERM.COND. VISCOSITY THERM.COND. SURF.TENSION
STAGE CENTIPOISE BTU/FT-HR-F CENTIPOISE BTU/FT-HR-F DYNE/CM
50 0.00914 0.01228 0.222 0.05765 15.51
49 0.00922 0.01251 0.217 0.05708 15.11
48 0.00922 0.01252 0.217 0.05704 15.09
47 0.00923 0.01253 0.217 0.05701 15.07
46 0.00923 0.01254 0.216 0.05699 15.05
45 0.00924 0.01256 0.216 0.05696 15.03
44 0.00924 0.01257 0.216 0.05693 15.01
43 0.00925 0.01258 0.216 0.05691 14.99
42 0.00925 0.01259 0.215 0.05688 14.97
41 0.00925 0.01260 0.215 0.05685 14.95
40 0.00926 0.01261 0.215 0.05683 14.94
39 0.00926 0.01262 0.215 0.05680 14.92
38 0.00927 0.01263 0.214 0.05677 14.90
37 0.00927 0.01264 0.214 0.05675 14.88
36 0.00928 0.01265 0.214 0.05672 14.86
35 0.00928 0.01266 0.214 0.05670 14.84
34 0.00928 0.01267 0.214 0.05667 14.82
33 0.00929 0.01268 0.213 0.05664 14.80
32 0.00929 0.01269 0.213 0.05661 14.78
31 0.00930 0.01270 0.213 0.05659 14.77
30 0.00930 0.01272 0.213 0.05656 14.75
29 0.00930 0.01273 0.213 0.05653 14.73
28 0.00931 0.01274 0.212 0.05650 14.71
27 0.00931 0.01275 0.212 0.05647 14.69
26 0.00932 0.01276 0.212 0.05644 14.67
25 0.00932 0.01277 0.212 0.05641 14.65
24 0.00932 0.01278 0.212 0.05638 14.62
23 0.00933 0.01279 0.211 0.05634 14.60
22 0.00933 0.01280 0.211 0.05631 14.58
21 0.00934 0.01281 0.211 0.05627 14.55
20 0.00934 0.01282 0.211 0.05623 14.53
19 0.00935 0.01283 0.211 0.05619 14.50
18 0.00935 0.01284 0.211 0.05614 14.47
17 0.00935 0.01286 0.211 0.05609 14.44
16 0.00936 0.01288 0.211 0.05601 14.40
15 0.00937 0.01292 0.211 0.05591 14.35
14 0.00937 0.01293 0.211 0.05585 14.32
13 0.00938 0.01294 0.211 0.05577 14.27
12 0.00938 0.01295 0.211 0.05568 14.22
11 0.00939 0.01297 0.211 0.05556 14.15
10 0.00939 0.01298 0.211 0.05541 14.06
9 0.00939 0.01300 0.212 0.05522 13.96
8 0.00940 0.01302 0.212 0.05500 13.82
7 0.00940 0.01304 0.213 0.05473 13.67
6 0.00941 0.01308 0.214 0.05441 13.49
5 0.00941 0.01313 0.214 0.05406 13.27
4 0.00941 0.01321 0.213 0.05365 13.02
3 0.00941 0.01331 0.212 0.05319 12.72
2 0.00941 0.01345 0.208 0.05271 12.39
1 0.00942 0.01369 0.208 0.05257 12.36
HEAT EXCHANGER BLOCK E105 EB product cooler, E-105
DUTY= 1.1819 MM BTU/HR
HOT SIDE INLET TEMP= 297.0 F, L/F=1.0000, FLOW= 13127.26 LB/HR
LIQUID DENSITY= 46.82 LB/FT3
OUTLET TEMP= 105.0 F, L/F=1.0000
LIQUID DENSITY= 53.19 LB/FT3
COLD SIDE INLET TEMP= 85.0 F, L/F=1.0000, FLOW= 59253.24 LB/HR
LIQUID DENSITY= 62.18 LB/FT3
OUTLET TEMP= 105.0 F, L/F=1.0000
LIQUID DENSITY= 61.95 LB/FT3
LMTD= 76.1 F, UNCORRECTED
MTD CORRECTION FACTOR (OVERALL, FOR EVEN TUBE PASS SHELLS):
0.829 FOR 1 SHELL
0.970 FOR 2 SHELLS
REQUIRED U*A= 15539.4 BTU/HR -F, BASED ON UNCORRECTED MTD
COLUMN BLOCK C103 PEB recovery column, C-103
COLUMN SUMMARY. FLOWS ARE IN LBMOL/HR
STAGE TEMP PRESS FLOW FROM STAGE FEED PRODUCT HEAT ADDED
F PSIG VAPOR LIQUID MM BTU/HR
10 261.1 -9.696 0.0 97.2 20.1 LIQ -2.230
9 283.0 -8.696 117.2 100.3
8 290.4 -8.571 120.4 100.6
7 294.6 -8.446 120.7 100.6
6 297.8 -8.321 120.7 113.9 21.4
5 301.5 -8.196 112.5 114.1
4 304.3 -8.071 112.8 112.1
3 312.2 -7.946 110.7 95.1
2 363.5 -7.821 93.8 74.5
1 447.2 -7.696 73.2 1.3 LIQ 2.070
FEED STREAM 7 TO STAGE 6 = 21.4 LBMOL/HR LIQUID STREAM 8 FROM STAGE 10 = 20.1 LBMOL/HR BOTTOMS STREAM 9 = 1.3 LBMOL/HR EXTERNAL REFLUX RATIO= 4.841 INTERNAL REFLUX RATIO= 5.000
--------------VAPOR------------- --------------LIQUID-------------
WT FLOW MW VOL FLOW DENSITY WT FLOW MW VOL FLOW DENSITY
STAGE LB/HR FT3/SEC LB/FT3 LB/HR GPM LB/FT3
10 0.0 123.6 0.00 0.0812 12423.5 127.9 32.14 48.2
9 14989.8 127.9 42.41 0.0982 13131.1 130.9 34.39 47.6
8 15697.4 130.4 43.07 0.1012 13314.8 132.3 34.99 47.4
7 15881.1 131.6 42.52 0.1037 13379.0 133.0 35.23 47.4
6 15945.3 132.1 41.84 0.1059 15232.8 133.8 40.09 47.4
5 14993.2 133.3 38.43 0.1084 15330.3 134.3 40.42 47.3
4 15090.7 133.8 37.91 0.1106 15116.4 134.9 39.87 47.3
3 14876.7 134.3 36.91 0.1119 13266.2 139.5 34.47 48.0
2 13026.6 138.9 32.79 0.1103 12179.1 163.4 29.84 50.9
1 11939.5 163.1 27.66 0.1199 239.6 179.1 0.59 51.0
--------VAPOR--------- --------------LIQUID------------------
VISCOSITY THERM.COND. VISCOSITY THERM.COND. SURF.TENSION
STAGE CENTIPOISE BTU/FT-HR-F CENTIPOISE BTU/FT-HR-F DYNE/CM
10 0.00809 0.01059 0.306 0.05955 17.89
9 0.00817 0.01117 0.287 0.05829 16.90
8 0.00815 0.01134 0.281 0.05790 16.60
7 0.00814 0.01143 0.277 0.05769 16.44
6 0.00815 0.01149 0.277 0.05764 16.40
5 0.00815 0.01155 0.273 0.05744 16.24
4 0.00816 0.01159 0.272 0.05736 16.18
3 0.00822 0.01168 0.284 0.05791 16.70
2 0.00866 0.01221 0.331 0.05998 18.87
1 0.00907 0.01323 0.291 0.05830 17.93
PUMP BLOCK P102 PEB recycle pump, P-102
HORSEPOWER = 2.4 AT 50.0 % EFFICIENCY
DRIVER POWER = 1.8 KILOWATT AT 100% EFFICIENCY
FLOW= 6.64 GAL/MIN, SPECIFIC GRAVITY= 0.7728
SUCTION PRESSURE= -9.696 PSIG, DISCHARGE PRESSURE= 300.00 PSIG
DISCHARGE TEMPERATURE= 264.2 F
CALCULATOR BLOCK SUMMARY Summary of process results
Reactor benzene preheating (via HPS): 4.42 MMBTU/hr
Fired heater: Benzene superheating: 10.11 MMBTU/hr
Recycle DEB vaporizing: 0.19 MMBTU/hr
Reboiler duties: Benzene column: 4.54 MMBTU/hr
EB column: 8.19 MMBTU/hr
PEB column: 2.07 MMBTU/hr
Total: 14.79 MMBTU/hr
Benzene column steam generation: 18.66 MMBTU/hr
EB product purity: 99.37 %
Benzene: 1213 ppm(wt)
Toluene: 3934 ppm(wt)
Xylenes: 1009 ppm(wt)
Cumene: 100 ppm(wt)
STREAM 1 Fresh benzene to process
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 134.253 0.9958 10487.02 0.9950
5 Toluene 0.572 0.424E-02 52.70 0.500E-02
------------ ------------
134.825 10539.72
TEMPERATURE 250.0 F PRESSURE 250.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 0.967 MMBTU/HR
AVERAGE MOL.WT. 78.17
VOLUME 27.43 GAL/MIN SPECIFIC GRAVITY 0.7682 ( 250.0 F)
23.88 GAL/MIN 0.8825 ( 60.0 F)
HEAT CAPACITY 0.4842 BTU/LB-F VISCOSITY 0.216 CENTIPOISE
SURFACE TENSION 16.12 DYNE/CM THERM.COND 0.06580 BTU/FT-HR-F
STREAM 2 Cold ethylene feed
LBMOL/HR MOL FR. LB/HR WT.FR.
2 Ethylene 124.511 0.9981 3493.00 0.9980
3 Ethane 0.233 0.187E-02 7.00 0.200E-02
------------ ------------
124.744 3500.00
TEMPERATURE 80.0 F PRESSURE 350.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 0.767 MMBTU/HR
AVERAGE MOL.WT. 28.06 DENSITY 2.091 LB/FT3
VOLUME 27.90 CFM COMPRESSIBILITY 0.8450
HEAT CAPACITY 0.4451 BTU/LB-F VISCOSITY 0.01113 CENTIPOISE
THERM.COND 0.01380 BTU/FT-HR-F
STREAM 2A Hot ethylene to reactor
LBMOL/HR MOL FR. LB/HR WT.FR.
2 Ethylene 124.511 0.9981 3493.00 0.9980
3 Ethane 0.233 0.187E-02 7.00 0.200E-02
------------ ------------
124.744 3500.00
TEMPERATURE 250.0 F PRESSURE 345.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 1.039 MMBTU/HR
AVERAGE MOL.WT. 28.06 DENSITY 1.400 LB/FT3
VOLUME 41.65 CFM COMPRESSIBILITY 0.9463
HEAT CAPACITY 0.4797 BTU/LB-F VISCOSITY 0.01375 CENTIPOISE
THERM.COND 0.02033 BTU/FT-HR-F
STREAM 3 Fresh & recycle benzene from benzene column
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.829 0.928E-03 1.67 0.239E-04
2 Ethylene 0.202 0.226E-03 5.65 0.809E-04
3 Ethane 1.213 0.136E-02 36.47 0.522E-03
4 Benzene 882.133 0.9876 68906.58 0.9864
5 Toluene 2.286 0.256E-02 210.66 0.302E-02
6 Ethylbenzene 6.580 0.737E-02 698.61 0.0100
7 m/p-Xylene 0.003 0.288E-05 0.27 0.390E-05
8 Cumene 0.000 0.255E-06 0.03 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.431E-12
------------ ------------
893.246 69859.95
TEMPERATURE 320.5 F PRESSURE 110.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 8.954 MMBTU/HR
AVERAGE MOL.WT. 78.21
VOLUME 194.84 GAL/MIN SPECIFIC GRAVITY 0.7168 ( 320.5 F)
158.48 GAL/MIN 0.8813 ( 60.0 F)
HEAT CAPACITY 0.5410 BTU/LB-F VISCOSITY 0.153 CENTIPOISE
SURFACE TENSION 11.60 DYNE/CM THERM.COND 0.05872 BTU/FT-HR-F
STREAM 3A Benzene from feed pump
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.829 0.928E-03 1.67 0.239E-04
2 Ethylene 0.202 0.226E-03 5.65 0.809E-04
3 Ethane 1.213 0.136E-02 36.47 0.522E-03
4 Benzene 882.133 0.9876 68906.58 0.9864
5 Toluene 2.286 0.256E-02 210.66 0.302E-02
6 Ethylbenzene 6.580 0.737E-02 698.61 0.0100
7 m/p-Xylene 0.003 0.288E-05 0.27 0.390E-05
8 Cumene 0.000 0.255E-06 0.03 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.431E-12
------------ ------------
893.246 69859.95
TEMPERATURE 323.0 F PRESSURE 335.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 9.050 MMBTU/HR
AVERAGE MOL.WT. 78.21
VOLUME 195.37 GAL/MIN SPECIFIC GRAVITY 0.7149 ( 323.0 F)
158.48 GAL/MIN 0.8813 ( 60.0 F)
HEAT CAPACITY 0.5369 BTU/LB-F VISCOSITY 0.151 CENTIPOISE
SURFACE TENSION 11.45 DYNE/CM THERM.COND 0.05847 BTU/FT-HR-F
STREAM 3B Benzene from feed preheater
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.829 0.928E-03 1.67 0.239E-04
2 Ethylene 0.202 0.226E-03 5.65 0.809E-04
3 Ethane 1.213 0.136E-02 36.47 0.522E-03
4 Benzene 882.133 0.9876 68906.58 0.9864
5 Toluene 2.286 0.256E-02 210.66 0.302E-02
6 Ethylbenzene 6.580 0.737E-02 698.61 0.0100
7 m/p-Xylene 0.003 0.288E-05 0.27 0.390E-05
8 Cumene 0.000 0.255E-06 0.03 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.431E-12
------------ ------------
893.246 69859.95
TEMPERATURE 430.0 F PRESSURE 330.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 13.471 MMBTU/HR
AVERAGE MOL.WT. 78.21
VOLUME 224.95 GAL/MIN SPECIFIC GRAVITY 0.6209 ( 430.0 F)
158.48 GAL/MIN 0.8813 ( 60.0 F)
HEAT CAPACITY 0.6647 BTU/LB-F VISCOSITY 0.098 CENTIPOISE
SURFACE TENSION 5.28 DYNE/CM THERM.COND 0.04802 BTU/FT-HR-F
STREAM 3C Benzene vapor from vaporizer
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.829 0.928E-03 1.67 0.239E-04
2 Ethylene 0.202 0.226E-03 5.65 0.809E-04
3 Ethane 1.213 0.136E-02 36.47 0.522E-03
4 Benzene 882.133 0.9876 68906.58 0.9864
5 Toluene 2.286 0.256E-02 210.66 0.302E-02
6 Ethylbenzene 6.580 0.737E-02 698.61 0.0100
7 m/p-Xylene 0.003 0.288E-05 0.27 0.390E-05
8 Cumene 0.000 0.255E-06 0.03 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.431E-12
------------ ------------
893.246 69859.95
TEMPERATURE 448.0 F PRESSURE 320.00 PSIG
FRACTION LIQUID 0.0232 ENTHALPY 21.354 MMBTU/HR
AVERAGE MOL.WT. 78.21
STREAM 3D Benzene for reactor bed 1 to fired heater
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.622 0.928E-03 1.25 0.239E-04
2 Ethylene 0.151 0.226E-03 4.24 0.809E-04
3 Ethane 0.909 0.136E-02 27.35 0.522E-03
4 Benzene 661.604 0.9876 51680.29 0.9864
5 Toluene 1.715 0.256E-02 158.02 0.302E-02
6 Ethylbenzene 4.935 0.737E-02 523.92 0.100E-01
7 m/p-Xylene 0.002 0.287E-05 0.20 0.390E-05
8 Cumene 0.000 0.255E-06 0.02 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.430E-12
------------ ------------
669.939 52395.29
TEMPERATURE 448.0 F PRESSURE 320.00 PSIG
FRACTION LIQUID 0.0254 ENTHALPY 16.003 MMBTU/HR
AVERAGE MOL.WT. 78.21
STREAM 3E Quench benzene for remaining reactor beds
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.207 0.928E-03 0.42 0.239E-04
2 Ethylene 0.050 0.226E-03 1.41 0.809E-04
3 Ethane 0.303 0.136E-02 9.12 0.522E-03
4 Benzene 220.535 0.9876 17226.76 0.9864
5 Toluene 0.572 0.256E-02 52.67 0.302E-02
6 Ethylbenzene 1.645 0.737E-02 174.64 0.100E-01
7 m/p-Xylene 0.001 0.287E-05 0.07 0.390E-05
8 Cumene 0.000 0.255E-06 0.01 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.430E-12
------------ ------------
223.313 17465.10
TEMPERATURE 448.0 F PRESSURE 320.00 PSIG
FRACTION LIQUID 0.0254 ENTHALPY 5.334 MMBTU/HR
AVERAGE MOL.WT. 78.21
STREAM 3F Benzene for reactor bed 1 from fired heater
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 0.622 0.928E-03 1.25 0.239E-04
2 Ethylene 0.151 0.226E-03 4.24 0.809E-04
3 Ethane 0.909 0.136E-02 27.35 0.522E-03
4 Benzene 661.604 0.9876 51680.29 0.9864
5 Toluene 1.715 0.256E-02 158.02 0.302E-02
6 Ethylbenzene 4.935 0.737E-02 523.92 0.100E-01
7 m/p-Xylene 0.002 0.287E-05 0.20 0.390E-05
8 Cumene 0.000 0.255E-06 0.02 0.392E-06
9 Diethylbenzenes 0.000 0.251E-12 0.00 0.430E-12
------------ ------------
669.939 52395.29
TEMPERATURE 810.0 F PRESSURE 285.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 26.113 MMBTU/HR
AVERAGE MOL.WT. 78.21 DENSITY 1.840 LB/FT3
VOLUME 474.70 CFM COMPRESSIBILITY 0.9351
HEAT CAPACITY 0.5563 BTU/LB-F VISCOSITY 0.01836 CENTIPOISE
THERM.COND 0.03140 BTU/FT-HR-F
STREAM 4 Hot reactor effluent
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 2.078 0.227E-02 4.19 0.552E-04
2 Ethylene 0.250 0.273E-03 7.01 0.923E-04
3 Ethane 1.445 0.158E-02 43.46 0.572E-03
4 Benzene 756.523 0.8281 59094.70 0.7783
5 Toluene 2.287 0.250E-02 210.69 0.277E-02
6 Ethylbenzene 130.795 0.1432 13886.08 0.1829
7 m/p-Xylene 0.132 0.144E-03 13.99 0.184E-03
8 Cumene 6.447 0.706E-02 774.84 0.0102
9 Diethylbenzenes 12.398 0.0136 1664.08 0.0219
10 Heavies 1.249 0.137E-02 227.60 0.300E-02
------------ ------------
913.602 75926.64
TEMPERATURE 811.1 F PRESSURE 230.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 38.678 MMBTU/HR
AVERAGE MOL.WT. 83.11 DENSITY 1.586 LB/FT3
VOLUME 797.91 CFM COMPRESSIBILITY 0.9403
HEAT CAPACITY 0.5655 BTU/LB-F VISCOSITY 0.01755 CENTIPOISE
THERM.COND 0.03124 BTU/FT-HR-F
STREAM 4A Reactor effluent from feed vaporizer
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 2.078 0.227E-02 4.19 0.552E-04
2 Ethylene 0.250 0.273E-03 7.01 0.923E-04
3 Ethane 1.445 0.158E-02 43.46 0.572E-03
4 Benzene 756.523 0.8281 59094.70 0.7783
5 Toluene 2.287 0.250E-02 210.69 0.277E-02
6 Ethylbenzene 130.795 0.1432 13886.08 0.1829
7 m/p-Xylene 0.132 0.144E-03 13.99 0.184E-03
8 Cumene 6.447 0.706E-02 774.84 0.0102
9 Diethylbenzenes 12.398 0.0136 1664.08 0.0219
10 Heavies 1.249 0.137E-02 227.60 0.300E-02
------------ ------------
913.602 75926.64
TEMPERATURE 619.2 F PRESSURE 225.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 30.795 MMBTU/HR
AVERAGE MOL.WT. 83.11 DENSITY 1.938 LB/FT3
VOLUME 653.07 CFM COMPRESSIBILITY 0.8880
HEAT CAPACITY 0.5183 BTU/LB-F VISCOSITY 0.01526 CENTIPOISE
THERM.COND 0.02377 BTU/FT-HR-F
STREAM 4B Reactor effluent from column reboiler
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 2.078 0.227E-02 4.19 0.552E-04
2 Ethylene 0.250 0.273E-03 7.01 0.923E-04
3 Ethane 1.445 0.158E-02 43.46 0.572E-03
4 Benzene 756.523 0.8281 59094.70 0.7783
5 Toluene 2.287 0.250E-02 210.69 0.277E-02
6 Ethylbenzene 130.795 0.1432 13886.08 0.1829
7 m/p-Xylene 0.132 0.144E-03 13.99 0.184E-03
8 Cumene 6.447 0.706E-02 774.84 0.0102
9 Diethylbenzenes 12.398 0.0136 1664.08 0.0219
10 Heavies 1.249 0.137E-02 227.60 0.300E-02
------------ ------------
913.602 75926.64
TEMPERATURE 500.0 F PRESSURE 220.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 26.258 MMBTU/HR
AVERAGE MOL.WT. 83.11 DENSITY 2.287 LB/FT3
VOLUME 553.22 CFM COMPRESSIBILITY 0.8280
HEAT CAPACITY 0.4897 BTU/LB-F VISCOSITY 0.01389 CENTIPOISE
THERM.COND 0.01956 BTU/FT-HR-F
STREAM 5 Benzene recovery column bottoms
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.204 0.140E-02 15.93 0.100E-02
5 Toluene 0.561 0.386E-02 51.65 0.324E-02
6 Ethylbenzene 124.195 0.8554 13185.41 0.8275
7 m/p-Xylene 0.129 0.890E-03 13.72 0.861E-03
8 Cumene 6.446 0.0444 774.81 0.0486
9 Diethylbenzenes 12.398 0.0854 1664.08 0.1044
10 Heavies 1.249 0.860E-02 227.60 0.0143
------------ ------------
145.182 15933.20
TEMPERATURE 475.1 F PRESSURE 117.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 3.960 MMBTU/HR
AVERAGE MOL.WT. 109.75
VOLUME 50.10 GAL/MIN SPECIFIC GRAVITY 0.6358 ( 475.1 F)
36.45 GAL/MIN 0.8738 ( 60.0 F)
HEAT CAPACITY 0.6464 BTU/LB-F VISCOSITY 0.141 CENTIPOISE
SURFACE TENSION 6.69 DYNE/CM THERM.COND 0.04447 BTU/FT-HR-F
STREAM 5A Benzene column bottoms fed to EB column
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.204 0.140E-02 15.93 0.100E-02
5 Toluene 0.561 0.386E-02 51.65 0.324E-02
6 Ethylbenzene 124.195 0.8554 13185.41 0.8275
7 m/p-Xylene 0.129 0.890E-03 13.72 0.861E-03
8 Cumene 6.446 0.0444 774.81 0.0486
9 Diethylbenzenes 12.398 0.0854 1664.08 0.1044
10 Heavies 1.249 0.860E-02 227.60 0.0143
------------ ------------
145.182 15933.20
TEMPERATURE 448.2 F PRESSURE 115.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 3.687 MMBTU/HR
AVERAGE MOL.WT. 109.75
VOLUME 48.55 GAL/MIN SPECIFIC GRAVITY 0.6561 ( 448.2 F)
36.45 GAL/MIN 0.8738 ( 60.0 F)
HEAT CAPACITY 0.6221 BTU/LB-F VISCOSITY 0.150 CENTIPOISE
SURFACE TENSION 7.94 DYNE/CM THERM.COND 0.04648 BTU/FT-HR-F
STREAM 6 Hot EB product from EB column
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.204 0.165E-02 15.93 0.121E-02
5 Toluene 0.561 0.453E-02 51.65 0.393E-02
6 Ethylbenzene 122.874 0.9927 13045.11 0.9937
7 m/p-Xylene 0.125 0.101E-02 13.26 0.101E-02
8 Cumene 0.011 0.882E-04 1.31 0.100E-03
9 Diethylbenzenes 0.000 0.114E-14 0.00 0.145E-14
------------ ------------
123.774 13127.26
TEMPERATURE 297.0 F PRESSURE 5.000 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 1.857 MMBTU/HR
AVERAGE MOL.WT. 106.06
VOLUME 34.96 GAL/MIN SPECIFIC GRAVITY 0.7508 ( 297.0 F)
30.01 GAL/MIN 0.8744 ( 60.0 F)
HEAT CAPACITY 0.5246 BTU/LB-F VISCOSITY 0.222 CENTIPOISE
SURFACE TENSION 15.51 DYNE/CM THERM.COND 0.05765 BTU/FT-HR-F
STREAM 6A Cool EB product to tankage
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.204 0.165E-02 15.93 0.121E-02
5 Toluene 0.561 0.453E-02 51.65 0.393E-02
6 Ethylbenzene 122.874 0.9927 13045.11 0.9937
7 m/p-Xylene 0.125 0.101E-02 13.26 0.101E-02
8 Cumene 0.011 0.882E-04 1.31 0.100E-03
9 Diethylbenzenes 0.000 0.114E-14 0.00 0.145E-14
------------ ------------
123.774 13127.26
TEMPERATURE 105.0 F PRESSURE 3.000 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 0.675 MMBTU/HR
AVERAGE MOL.WT. 106.06
VOLUME 30.77 GAL/MIN SPECIFIC GRAVITY 0.8528 ( 105.0 F)
30.01 GAL/MIN 0.8744 ( 60.0 F)
HEAT CAPACITY 0.4130 BTU/LB-F VISCOSITY 0.529 CENTIPOISE
SURFACE TENSION 26.83 DYNE/CM THERM.COND 0.07234 BTU/FT-HR-F
STREAM 7 EB recovery column bottoms
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.000 0.435E-12 0.00 0.259E-12
5 Toluene 0.000 0.241E-07 0.00 0.170E-07
6 Ethylbenzene 1.321 0.0617 140.30 0.0500
7 m/p-Xylene 0.004 0.205E-03 0.46 0.166E-03
8 Cumene 6.435 0.3006 773.50 0.2757
9 Diethylbenzenes 12.398 0.5791 1664.08 0.5931
10 Heavies 1.249 0.0583 227.60 0.0811
------------ ------------
21.408 2805.94
TEMPERATURE 382.1 F PRESSURE 12.000 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 0.584 MMBTU/HR
AVERAGE MOL.WT. 131.07
VOLUME 7.81 GAL/MIN SPECIFIC GRAVITY 0.7186 ( 382.1 F)
6.41 GAL/MIN 0.8751 ( 60.0 F)
HEAT CAPACITY 0.5686 BTU/LB-F VISCOSITY 0.208 CENTIPOISE
SURFACE TENSION 12.36 DYNE/CM THERM.COND 0.05257 BTU/FT-HR-F
STREAM 8 PEB column distillate
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.000 0.464E-12 0.00 0.284E-12
5 Toluene 0.000 0.258E-07 0.00 0.186E-07
6 Ethylbenzene 1.321 0.0658 140.30 0.0547
7 m/p-Xylene 0.004 0.218E-03 0.46 0.181E-03
8 Cumene 6.435 0.3206 773.48 0.3014
9 Diethylbenzenes 12.309 0.6133 1652.10 0.6438
10 Heavies 0.000 0.664E-07 0.00 0.946E-07
------------ ------------
20.070 2566.34
TEMPERATURE 261.1 F PRESSURE -9.696 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 0.373 MMBTU/HR
AVERAGE MOL.WT. 127.87
VOLUME 6.64 GAL/MIN SPECIFIC GRAVITY 0.7728 ( 261.1 F)
5.92 GAL/MIN 0.8665 ( 60.0 F)
HEAT CAPACITY 0.5073 BTU/LB-F VISCOSITY 0.306 CENTIPOISE
SURFACE TENSION 17.89 DYNE/CM THERM.COND 0.05955 BTU/FT-HR-F
STREAM 8A Recycle PEB from pump
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.000 0.464E-12 0.00 0.284E-12
5 Toluene 0.000 0.258E-07 0.00 0.186E-07
6 Ethylbenzene 1.321 0.0658 140.30 0.0547
7 m/p-Xylene 0.004 0.218E-03 0.46 0.181E-03
8 Cumene 6.435 0.3206 773.48 0.3014
9 Diethylbenzenes 12.309 0.6133 1652.10 0.6438
10 Heavies 0.000 0.664E-07 0.00 0.946E-07
------------ ------------
20.070 2566.34
TEMPERATURE 264.2 F PRESSURE 300.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 0.379 MMBTU/HR
AVERAGE MOL.WT. 127.87
VOLUME 6.65 GAL/MIN SPECIFIC GRAVITY 0.7712 ( 264.2 F)
5.92 GAL/MIN 0.8665 ( 60.0 F)
HEAT CAPACITY 0.5071 BTU/LB-F VISCOSITY 0.302 CENTIPOISE
SURFACE TENSION 17.72 DYNE/CM THERM.COND 0.05935 BTU/FT-HR-F
STREAM 8B Recycle PEB from heater
LBMOL/HR MOL FR. LB/HR WT.FR.
4 Benzene 0.000 0.463E-12 0.00 0.283E-12
5 Toluene 0.000 0.257E-07 0.00 0.185E-07
6 Ethylbenzene 1.321 0.0658 140.28 0.0547
7 m/p-Xylene 0.004 0.218E-03 0.46 0.181E-03
8 Cumene 6.435 0.3206 773.46 0.3014
9 Diethylbenzenes 12.309 0.6133 1652.10 0.6438
10 Heavies 0.000 0.664E-07 0.00 0.946E-07
------------ ------------
20.070 2566.30
TEMPERATURE 400.0 F PRESSURE 280.00 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 0.569 MMBTU/HR
AVERAGE MOL.WT. 127.87
VOLUME 7.36 GAL/MIN SPECIFIC GRAVITY 0.6971 ( 400.0 F)
5.92 GAL/MIN 0.8665 ( 60.0 F)
HEAT CAPACITY 0.5809 BTU/LB-F VISCOSITY 0.189 CENTIPOISE
SURFACE TENSION 10.89 DYNE/CM THERM.COND 0.05071 BTU/FT-HR-F
STREAM 9 Process residue
LBMOL/HR MOL FR. LB/HR WT.FR.
5 Toluene 0.000 0.203E-13 0.00 0.104E-13
6 Ethylbenzene 0.000 0.208E-05 0.00 0.123E-05
7 m/p-Xylene 0.000 0.105E-07 0.00 0.622E-08
8 Cumene 0.000 0.141E-03 0.02 0.947E-04
9 Diethylbenzenes 0.089 0.0667 11.98 0.0500
10 Heavies 1.249 0.9331 227.60 0.9499
------------ ------------
1.338 239.61
TEMPERATURE 447.2 F PRESSURE -7.696 PSIG
FRACTION LIQUID 1.0000 ENTHALPY 50877.3 BTU/HR
AVERAGE MOL.WT. 179.05
VOLUME 0.59 GAL/MIN SPECIFIC GRAVITY 0.8171 ( 447.2 F)
0.49 GAL/MIN 0.9843 ( 60.0 F)
HEAT CAPACITY 0.5362 BTU/LB-F VISCOSITY 0.291 CENTIPOISE
SURFACE TENSION 17.93 DYNE/CM THERM.COND 0.05830 BTU/FT-HR-F
STREAM 10 Vent from benzene column
LBMOL/HR MOL FR. LB/HR WT.FR.
1 Hydrogen 1.249 0.1249 2.52 0.374E-02
2 Ethylene 0.048 0.482E-02 1.35 0.201E-02
3 Ethane 0.233 0.0233 6.99 0.0104
4 Benzene 8.439 0.8439 659.22 0.9792
5 Toluene 0.012 0.117E-02 1.08 0.160E-02
6 Ethylbenzene 0.019 0.195E-02 2.07 0.307E-02
7 m/p-Xylene 0.000 0.717E-06 0.00 0.113E-05
8 Cumene 0.000 0.478E-07 0.00 0.853E-07
9 Diethylbenzenes 0.000 0.244E-13 0.00 0.486E-13
------------ ------------
10.000 673.23
TEMPERATURE 320.5 F PRESSURE 110.00 PSIG
FRACTION LIQUID 0.0000 ENTHALPY 0.189 MMBTU/HR
AVERAGE MOL.WT. 67.32 DENSITY 1.119 LB/FT3
VOLUME 10.02 CFM COMPRESSIBILITY 0.8958
HEAT CAPACITY 0.4074 BTU/LB-F VISCOSITY 0.01158 CENTIPOISE
THERM.COND 0.01697 BTU/FT-HR-F
HEAT CURVE FOR STREAM 4 AT PRESSURE= 220.00 PSIG
DEW POINT= 445.3 F ENTHALPY= 0.2425E+08 BTU/HR
BUBBLE POINT= 402.2 F ENTHALPY= 0.1379E+08 BTU/HR
PSEUDO-CRITICAL (MOLAR AVERAGED) TEMP= 567.2 F, PRESS= 660.93 PSIG
DUTIES REFERENCED TO ENTHALPY= 0.3868E+08 BTU/HR AT TEMP= 811.1 F,
PRESS= 230.00 PSIG, L/F = 0.0000, FLOWRATE= 75926.6 LB/HR
WT. FREE ENTHALPY ENTHALPY HEAT HEAT CAPAC. VAP. DENSITY MOL VISCOSITY THERM.COND. SURF. TEMP. FRAC. WATER CHANGE, CHANGE, OF BTU/LB-F AVG. LB/FT3 FRAC. (CP) (CP) BTU/FT-HR-F TENS. DEG F VAPOR LB/HR MMBTU/HR BTU/LB VAP. VAP. LIQ. M.W. VAP. LIQ. LIQ. VAP. LIQ. VAP. LIQ. DYN/CM ----- ------ ----- --------- ------- ----- ----- ----- ----- ------ ------ ----- ------- ------ ------ ------ ------ 810.6 1.0000 0.0000 0.00 0.565 83.1 1.5180 0.000 0.01751 0.0312 800.6 1.0000 -0.4278 -5.63 0.562 83.1 1.5331 0.000 0.01739 0.0308 790.6 1.0000 -0.8538 -11.25 0.560 83.1 1.5487 0.000 0.01727 0.0304 780.6 1.0000 -1.2780 -16.83 0.558 83.1 1.5646 0.000 0.01715 0.0300 770.6 1.0000 -1.7004 -22.40 0.555 83.1 1.5808 0.000 0.01703 0.0296 760.6 1.0000 -2.1210 -27.93 0.553 83.1 1.5976 0.000 0.01691 0.0292 750.6 1.0000 -2.5397 -33.45 0.550 83.1 1.6147 0.000 0.01680 0.0288 740.6 1.0000 -2.9566 -38.94 0.548 83.1 1.6323 0.000 0.01668 0.0284 730.6 1.0000 -3.3716 -44.41 0.546 83.1 1.6504 0.000 0.01656 0.0280 720.6 1.0000 -3.7848 -49.85 0.543 83.1 1.6689 0.000 0.01644 0.0276 710.6 1.0000 -4.1961 -55.27 0.541 83.1 1.6880 0.000 0.01632 0.0272 700.6 1.0000 -4.6055 -60.66 0.538 83.1 1.7077 0.000 0.01620 0.0268 690.6 1.0000 -5.0130 -66.02 0.536 83.1 1.7279 0.000 0.01608 0.0264 680.6 1.0000 -5.4187 -71.37 0.533 83.1 1.7487 0.000 0.01596 0.0261 670.6 1.0000 -5.8224 -76.69 0.531 83.1 1.7702 0.000 0.01585 0.0257 660.6 1.0000 -6.2243 -81.98 0.528 83.1 1.7923 0.000 0.01573 0.0253 650.6 1.0000 -6.6242 -87.24 0.526 83.1 1.8152 0.000 0.01561 0.0249 640.6 1.0000 -7.0222 -92.49 0.523 83.1 1.8388 0.000 0.01549 0.0245 630.6 1.0000 -7.4184 -97.70 0.521 83.1 1.8632 0.000 0.01538 0.0242 620.6 1.0000 -7.8126 -102.90 0.518 83.1 1.8885 0.000 0.01526 0.0238 610.6 1.0000 -8.2049 -108.06 0.516 83.1 1.9146 0.000 0.01514 0.0234 600.6 1.0000 -8.5953 -113.20 0.513 83.1 1.9417 0.000 0.01503 0.0231 590.6 1.0000 -8.9838 -118.32 0.511 83.1 1.9699 0.000 0.01491 0.0227 580.6 1.0000 -9.3704 -123.41 0.508 83.1 1.9992 0.000 0.01479 0.0224 570.6 1.0000 -9.7552 -128.48 0.506 83.1 2.0296 0.000 0.01468 0.0220 560.6 1.0000 -10.1381 -133.52 0.503 83.1 2.0613 0.000 0.01457 0.0216 550.6 1.0000 -10.5192 -138.54 0.501 83.1 2.0944 0.000 0.01445 0.0213 540.6 1.0000 -10.8984 -143.54 0.499 83.1 2.1290 0.000 0.01434 0.0209 530.6 1.0000 -11.2760 -148.51 0.496 83.1 2.1651 0.000 0.01423 0.0206 520.6 1.0000 -11.6518 -153.46 0.494 83.1 2.2031 0.000 0.01411 0.0203 510.6 1.0000 -12.0259 -158.39 0.492 83.1 2.2429 0.000 0.01400 0.0199 500.6 1.0000 -12.3984 -163.29 0.490 83.1 2.2849 0.000 0.01389 0.0196 490.6 1.0000 -12.7694 -168.18 0.488 83.1 2.3292 0.000 0.01379 0.0193 480.6 1.0000 -13.1390 -173.05 0.486 83.1 2.3761 0.000 0.01368 0.0189 470.6 1.0000 -13.5072 -177.90 0.484 83.1 2.4259 0.000 0.01357 0.0186 460.6 1.0000 -13.8743 -182.73 0.483 83.1 2.4788 0.000 0.01347 0.0183 450.6 1.0000 -14.2404 -187.55 0.482 83.1 2.5355 0.000 0.01336 0.0180 445.3 *1.0000 -14.4330 -190.09 108.9 0.481 0.639 83.1 2.5670 39.8 0.000 0.01331 0.112 0.0178 0.0473 6.3