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Synthesis of Tetrahydrofuran
Designed for Claire and Charlie’s Chemicals, Inc.
TIGER STYLE CHEMICAL
December 7, 2011
Laura Chong, Cody Farinella, Andrew Nandor, Laura Musick, Jing Wang
1
Tiger Style Chemical
December 7, 2011
Tiger Style Chemical
W1225 Lafferre Hall
Columbia, MO 65211
Dear Claire and Charlie’s Chemicals, Inc.,
We would like to present to you our complete process design for the production of
tetrahydrofuran from n-butane. Our company prides itself in thorough, quality work that you
will find in the report we have created for you. If you have any questions please do not hesitate
to contact any of the members below.
Thank you for choosing Tiger Style Chemical for your design needs and we look forward to
working with you again.
Sincerely,
Laura Chong Jing Wang
Project Engineer Project Engineer
Cody Farinella Andrew Nandor
Process Engineer Process Engineer
Laura Musick
Chief Economic Analyst
2
Contents
Executive Summary ........................................................................................................................ 3
Background ..................................................................................................................................... 4
Methods........................................................................................................................................... 5
Production of Maleic Anhydride from n-Butane ........................................................................ 7
Production of Tetrahydrofuran from Maleic Anhydride ............................................................ 8
Stream Table ............................................................................................................................... 9
Results ........................................................................................................................................... 19
Equipment Summary ................................................................................................................ 20
Capital and Manufacturing Costs.............................................................................................. 25
Optimization ................................................................................................................................. 30
Safety and Environmental ............................................................................................................. 32
Chemical Hazards ..................................................................................................................... 33
Process Hazards ........................................................................................................................ 33
Waste Treatment ....................................................................................................................... 33
Conclusion .................................................................................................................................... 34
References ..................................................................................................................................... 35
Appendix A – Sample Calculations .............................................................................................. 37
Mass and Energy Balances ....................................................................................................... 37
Overall................................................................................................................................... 37
Reboiler and Reflux Streams ................................................................................................ 40
Heat Integration .................................................................................................................... 42
Equipment Sizing ...................................................................................................................... 49
Capital and Manufacturing Costs.............................................................................................. 54
Appendix B – Aspen Input Summaries ........................................................................................ 74
Production of Maleic Anhydride from n-Butane ...................................................................... 74
Production of Tetrahydrofuran from Maleic Anhydride ........................................................ 101
Appendix C – Material Saftey Data Sheet .................................................................................. 126
3
Executive Summary
The process designed produces pure Tetrahydrofuran from n-butane. The total grass roots cost
for the construction of the plant and process equipment is $54,936,336 with an operating cost of
$65,127,255 per year. After ten years, with a revenue of $47,523,000, the net present value is
-$67,659,173. This process, unfortunately, is not profitable. We have presented an optimization
case of purifying one of the purge streams which adds an additional $1.7 million to the cost of
manufacture and brings the net present value to -$52,369,898, over $15 million dollars closer to
a profitable process. We believe that this is not a profitable process because of the high cost of
pure hydrogen and suggest exploring further optimizations and more profitable end products.
4
Background
This process is made up of two reactions. Initially maleic anhydride (MAH) is produced from n-
butane. A feed stream of n-butane and air is sent through a reactor feed preparation stage and
then to Reactor 101. The reactions for the production of maleic anhydride from n-butane are
shown below, (equations 1-4).20
N-butane has an 82.2% single pass conversion. Maleic
anhydride has a selectivity of 70% in Reactor 1 and the selectivities of reactions 2-4 are each
10%. These values were obtained using a vanadium and phosphorus oxide catalyst (V-P-O).3
Reactor 101:
(1)
(2)
(3)
(4)
After the first reaction, the mixture is sent to an absorption column where the light components
are vaporized, and separated. Water is added at this stage to condense the heavy liquid.
Reaction 5 is just the hydration of maleic anhydride to maleic acid. This change occurs in the
absorptions column as the water stream comes into contact with the input stream. The absorption
liquid will retain 99.9 mass% of the maleic acid.16
Absorption column:
(5)
The mixture exits the absorber and it sent to a flash drum that removes water and other
byproducts. Reactor 102 is then used to convert all of the maleic acid back to maleic anhydride
since that it what’s need for the second part of this process. Reaction 6 below shows just that.
Reactor 102:
(6)
Finally the mixture is sent through a distillation tower that further purifies the maleic anhydride.
At this point the final product stream will be approximately 99.7% maleic anhydride. The final
product stream of this half of the process becomes the feed stream into the second half of the
process.
Once maleic anhydride is produced from n-butane, tetrahydrofuran (THF) is then produced from
the maleic anhydride. The feed from Distillation Tower 103 goes into a reactor feed prep. The
mixture is then sent to Reactor 201. Within Reactor 201, Reactions 7-10 occur. There is a 100%
conversion of maleic anhydride with a 98% selectivity of THF.4
5
Reactor 201:
(7)
(8)
(9)
(10)
The products of Reactor 201 are sent to an extraction tower where 99.9% of the hydrogen is
removed. In order to break the azeotrope between water and THF, a pressure swing distillation
will be used.12
Water will be removed from the bottoms of Distillation Tower 201 where the
distillate will contain 95% THF and will be sent to Distillation Tower 202. The bottoms of
Distillation Tower 202 will contain pure THF and the distillate will be recycled back to
Distillation Tower 201.
Methods
To simulate this process we used Aspen Plus. A picture of the Aspen simulation as well as the
stream table is shown on the following pages. For convenience, the first and second reaction
parts are separated. The input summaries may be found in Appendix B.
Sizing calculations were based off of values generated in Aspen.
Production of Maleic Anhydride from n-Butane.
The NRTL property method was used in the simulation. Indeed, Peng-Rob and NRTL both work
well, but in order to cooperate with the 2nd
part of the whole process, we choose NRTL.
In the real process, the reaction of MAH changing to maleic acid will occur. The Aspen
simulation does not show the reaction happening in an absorption tower, so we had to add a
reactor to simulate this process. For the absorption column, Aspen simulates this as a RadFrac
distillation column setting the reboiler and condenser to zero. The absorption tower allows the
MAH to be separated from the non-condensable gases.
For the reaction between MAH and water, we assume on the certain condition, the conversion is
100%, because MAH reacts readily with water, and when the condition changed, it can also very
easy to change back. We originally consider using a flash vessel to remove water, which works
better in the ASPEN simulation, but in the real process, it is not typically done. We changed this
to a distillation column which works just as well.
6
For the distillation towers to remove water (T-102) and purify MAH (T-103), we first used the
DSTWU model to get the estimated relative data. Then apply the basic data to the more
sophisticated RadFrac model to obtain better results.
The reactor temperature and pressure, 410°F and 39.875 psia, were taken from established
patents.3
Production of Tetrahydrofuran from Maleic Anhydride
The property method used in the second half is the NRTL method. It was compared with the
Peng-Rob and Wilson and showed to estimate the conditions at the water THF azeotrope closest
to the values found in literature.
The RStoic Reactor was chosen to represent our reactor because it was able to accurately deliver
the results that the patent for the catalyst claimed. This patent also justifies the choices for the
reactor temperature and pressures.
The pressure swing distillation configuration was based on the literature describing the process
for breaking the water and THF azeotrope. It described the pressures of each tower and the need
mole fractions desired at the tops and bottoms of each.
There were originally turbines in the places that a pressure drop was needed but after economic
analysis it was found to be more efficient to just have valves in their place.
7
Production of Maleic Anhydride from n-Butane
7
8
2
1
9
12
13
15A
15 17
22
2627
28
33
37
10
11
R-101
M-101
E-102 T-101
H-103
T-101R
R-102E-105
T-103
E-101P-101
T -101 & T -101R are in
the same one block in
the real process.
Vent t o Flare
Use V-O-P catalyst
in this reactor.
n-But ane
Air
Purif ied Process Water
T o PrimaryWaste
Wat er Treatment
T-102P-103
16
C-101
H-102
5
6
P-102
H-101
34
MAH to 2nd part
Figure 1. Aspen simulation of the production of maleic anhydride from n-butane.
8
Production of Tetrahydrofuran from Maleic Anhydride
Figure 2. Aspen simulation of the production of tetrahydrofuran from maleic anhydride.
36
42
49
43
44
51
52
78
56
60
61
66
74
73
45
50
46
47
48
77
70 71 72
62
M-201R-201
E-203
E-205T-201
S-202
V-201
S-201
E-204
V-204
T-202
CV-203E-211
C-201
C-202
C-203
Hydrogen
E-21075
76
39
T-103P
37
E-20238
E-201
41
CV-201
40
CV-202
CV-204
Note: T-103Prepresents T-103Bottoms Pump from 1st half
MAH from 1st Half
9
Stream Table
Table 1. Complete stream table.
Stream No. 1 2 3 4 5 6 7 8
Temperature °F 70 68 70 770 320 770 770 770
Pressure psia 31 15 40 40 40 40 40 40
Vapor Frac 0.00 1.00 0.00 1.00 1.00 1.00 1.00 1.00
Mole Flow lbmol/hr 95 2946 95 95 2946 2946 3041 3116
Mass Flow lb/hr 5500 84736 5500 5500 84736 84736 90237 90237
Volume Flow cuft/hr 152 1128860 152 31310 618018 974741 1006050 1030930
Enthalpy MMBtu/hr -6.00 -3.24 -6.00 -2.85 1.97 11.58 8.73 -46.56
Mass Flow lb/hr
THF
MAH 7627.86
BUTANE 5500.45 5500.45 5500.45 5500.45 5.52
OXYGEN
N2 64436.36 64436.36 64436.36 64436.36 64436.36
CO 775.69
CO2 50.33 50.33 50.33 50.33 1435.49
WATER 495.20 495.20 495.20 495.20 7512.83
MA
FORMIC 20.19
ACRYLIC 177.61
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF
MAH 0.085
BUTANE 1.000 1.000 1.000 0.061
OXYGEN 0.233 0.233 0.233 0.219 0.091
N2
CO 0.009
CO2 594 PPM 594 PPM 594 PPM 558 PPM 0.016
WATER 0.006 0.006 0.006 0.005 0.083
MA
FORMIC 224 PPM
ACRYLIC 0.002
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
10
Stream No. 9 10 11 12 13 15 15a 16
Temperature °F 203 59 59 203 158 203 155 203
Pressure psia 25 15 25 25 25 25 25 29
Vapor Frac 0.98 0.00 0.00 0.00 1.00 0.00 0.00 0.00
Mole Flow lbmol/hr 3116 1715 1715 1715 3206 1547 1624 1547
Mass Flow lb/hr 90237 30887 30887 30887 85468 35656 35656 35656
Volume Flow cuft/hr 881515 493 493 536 862148 588 558 588
Enthalpy MMBtu/hr -62.16 -211.08 -211.08 -206.75 -66.25 -202.51 -202.66 -202.51
Mass Flow lb/hr
THF
MAH 7627.86 0.00 7627.85
BUTANE 5.52 4.89 0.63 0.63 0.63
OXYGEN 8245.20 8238.82 6.38 6.38 6.38
N2 64436.36 64393.97 42.40 42.40 42.40
CO 775.69 775.15 0.54 0.54 0.54
CO2 1435.49 1427.22 8.27 8.27 8.27
WATER 7512.83 30887.20 30887.20 30887.20 10623.85 26374.79 27776.18 26374.79
MA 9029.24 9029.24
FORMIC 20.19 0.79 19.40 19.40 19.40
ACRYLIC 177.61 3.66 173.95 173.95 173.95
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF
MAH 0.085 47 PPB 0.214
BUTANE 57 PPM 18 PPM 18 PPM 18 PPM
OXYGEN 0.091 0.096 179 PPM 179 PPM 179 PPM
N2 0.714 0.753 0.001 0.001 0.001
CO 0.009 0.009 15 PPM 15 PPM 15 PPM
CO2 0.016 0.017 232 PPM 232 PPM 232 PPM
WATER 0.083 1.000 1.000 1.000 0.124 0.740 0.779 0.740
MA 0.253 0.253
FORMIC 224 PPM 9 PPM 544 PPM 544 PPM 544 PPM
ACRYLIC 0.002 43 PPM 0.005 0.005 0.005
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
11
Stream No. 17 18 19 20 21 22 23 24
Temperature °F 572 248 165 165 165 165 260 448
Pressure psia 29 26 24.5 24.5 29 29 26 24.5
Vapor Frac 0.00 0.94 0.00 0.00 0.00 0.00 0.35 0.62
Mole Flow lbmol/hr 1547 1551 1551 1551 1551 1463 1371 1371
Mass Flow lb/hr 35656 28093 28093 28093 28093 26503 37472 37472
Volume Flow cuft/hr 837 476 476 476 476 449 635 635
Enthalpy MMBtu/hr -186.23 -148.37 -177.36 -177.36 -177.36 -177.36 -355.25 -278.09
Mass Flow lb/hr
THF
MAH
BUTANE 0.63 0.63
OXYGEN 6.38 6.38
N2 42.40 56.19 56.19 56.19 56.19 42.40
CO 0.54 0.54
CO2 8.27 8.27
WATER 26374.79 27868.23 27868.23 27868.23 27868.23 26278.65 23785.44 23785.44
MA 9029.24 0.02 11272.79 11272.79
FORMIC 19.40 18.21 184.84 184.84
ACRYLIC 173.95 168.56 168.56 168.56 168.56 147.70 2229.13 2229.13
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF
MAH
BUTANE 18 PPM 24 PPM 24 PPM 24 PPM 24 PPM 24 PPM
OXYGEN 179 PPM 241 PPM 241 PPM 241 PPM 241 PPM 241 PPM
N2 0.001 0.002 0.002 0.002 0.002 0.002
CO 15 PPM 20 PPM 20 PPM 20 PPM 20 PPM 20 PPM
CO2 232 PPM 312 PPM 312 PPM 312 PPM 312 PPM 312 PPM
WATER 0.740 0.992 0.992 0.992 0.992 0.992 0.635 0.635
MA 0.253 884 PPB 884 PPB 884 PPB 884 PPB 884 PPB 0.301 0.301
FORMIC 544 PPM 687 PPM 687 PPM 687 PPM 687 PPM 687 PPM 0.005 0.005
ACRYLIC 0.005 0.006 0.006 0.006 0.006 0.006 0.059 0.059
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
12
Stream No. 25 26 27 28 29 30 31 32
Temperature °F 448 448 104 104 248 248 248 249
Pressure psia 26.0 29.0 29.0 29.0 26.0 26.0 26.0 29.0
Vapor Frac 0.00 0.00 0.00 0.00 0.91 0.00 0.00 0.00
Mole Flow lbmol/hr 84 84 84 161 92 92 92 92
Mass Flow lb/hr 9153 9153 9153 9153 1661 1661 1661 1661
Volume Flow cuft/hr 129 129 107 111 28 28 28 28
Enthalpy MMBtu/hr -25.064 -25.064 -26.598 -25.259 -8.39 -9.96 -9.96 -9.96
Mass Flow lb/hr
THF
MAH 7627.83
BUTANE TRACE TRACE TRACE
OXYGEN TRACE TRACE TRACE
N2 TRACE TRACE TRACE
CO TRACE TRACE TRACE
CO2 TRACE TRACE TRACE
WATER 96.13 96.13 96.13 1497.52 1650.83 1651.03 1651.03 1651.03
MA 9029.22 9029.22 9029.22
FORMIC 1.19 1.19 1.19 1.19
ACRYLIC 26.25 26.25 26.25 26.25 8.30 8.31 8.31 8.31
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF
MAH 0.833 453 PPB 453 PPB 453 PPB 453 PPB
BUTANE TRACE TRACE
OXYGEN TRACE TRACE TRACE
N2 TRACE TRACE TRACE
CO TRACE TRACE TRACE
CO2 TRACE TRACE TRACE
WATER 0.011 0.011 0.011 0.164 0.994 0.994 0.994 0.994
MA 0.986 0.986 0.986
FORMIC 130 PPM 130 PPM 130 PPM 130 PPM 765 PPM 765 PPM 765 PPM 765 PPM
ACRYLIC 0.003 0.003 0.003 0.003 0.005 0.005 0.005 0.005
H2
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
13
Stream No. 33 34 35 36 37 38 39 40
Temperature °F 249 433 444 444 445 464 70 70
Pressure psia 29 26 24.5 500 615 615 3500 614.7
Vapor Frac 0.00 0.37 0.64 0.00 0.00 0.00 1.00 1.00
Mole Flow lbmol/hr 83 220 220 78 78 78 426 426
Mass Flow lb/hr 1505 21286 21286 7648 7648 7648 858 858
Volume Flow cuft/hr 27 361 361 111 111 112 691 3937
Enthalpy MMBtu/hr -9.96 -1.06E+10 -7.17E+09 -13.984 -13.981 -13.909 -0.02 -0.02
Mass Flow lb/hr
THF
MAH 0.00 21071.51 21071.51 7627.81 7627.8 7627.81
BUTANE
OXYGEN
N2
CO
CO2
WATER 1495.87 42.65 42.65 1.621 1.621 1.621
MA
FORMIC 1.15 0.046 0.046 0.046
ACRYLIC 7.81 171.20 171.20 18.448 18.448 18.448
H2 858.233 858.233
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF
MAH 453 PPB 0.990 0.990 0.997 0.997 0.997
BUTANE
OXYGEN
N2
CO
CO2
WATER 0.994 0.002 0.002
212
PPM 212 PPM 212 PPM
MA
FORMIC 765 PPM 6 PPM 6 PPM 6 PPM
ACRYLIC 0.005 0.008 0.008 0.002 0.002 0.002
H2 1 1
BUTANOL
PROPANOL
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
14
Stream No. 41 42 43 44 45 46 47 48
Temperature °F 464 420 464 104 104 104 104 229
Pressure psia 614.7 614.7 614.7 362.6 362.6 362.6 362.6 616.2
Vapor Frac 1.00 0.87 1.00 0.75 1.00 1.00 1.00 1.00
Mole Flow lbmol/hr 426 504 928 928 694 35 660 660
Mass Flow lb/hr 858 8506 10447 10447 2043 102 1941 1941
Volume Flow cuft/hr 6865 6849 14972 11728 11584 579 11005 7909
Enthalpy MMBtu/hr 1.147 -12.762 -20.093 -27.074 -0.767 -0.038 -0.729 -0.142
Mass Flow lb/hr
THF 6079.498 6079.498 626.115 31.306 594.809 594.809
MAH 7627.813
BUTANE 1.749 1.749 0.291 0.015 0.276 0.276
OXYGEN
N2
CO
CO2 3.164 3.164 2.609 0.13 2.479 2.479
WATER 1.621 2837.164 2837.164 34.606 1.73 32.876 32.876
MA
FORMIC 0.046 0.046 0.046 <0.001 <0.001 <0.001 <0.001
ACRYLIC 18.448 18.463 18.463 0.016 0.001 0.015 0.015
H2 858.233 858.233 1380.055 1380.055 1378.238 68.912 1309.326 1309.326
BUTANOL 125.556 125.556 0.785 0.039 0.746 0.746
PROPANOL 0.949 0.949 0.015 0.001 0.014 0.014
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF 0.582 0.582 0.307 0.307 0.307 0.307
MAH 0.897
BUTANE 167 PPM 167 PPM 142 PPM 142 PPM 142 PPM 142 PPM
OXYGEN
N2
CO
CO2 303 PPM 303 PPM 0.001 0.001 0.001 0.001
WATER 191 PPM 0.272 0.272 0.017 0.017 0.017 0.017
MA
FORMIC 5 PPM 4 PPM 4 PPM 134 PPB 134 PPB 134 PPB 134 PPB
ACRYLIC 0.002 0.002 0.002 8 PPM 8 PPM 8 PPM 8 PPM
H2 1 0.101 0.132 0.132 0.675 0.675 0.675 0.675
BUTANOL 0.012 0.012 384 PPM 384 PPM 384 PPM 384 PPM
PROPANOL 91 PPM 91 PPM 7 PPM 7 PPM 7 PPM 7 PPM
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
15
Stream No. 49 50 51 52 53 54 55 56
Temperature °F 464 104 103 176 145 145 145 145
Pressure psia 614.7 362.6 16.0 14.5 13.5 12.0 12.0 14.5
Vapor Frac 1.00 0.00 0.01 0.62 0.60 0.33 0.60 1.00
Mole Flow lbmol/hr 660 234 234 234 1637 1637 1637 617
Mass Flow lb/hr 1940 8404 8404 8404 116082 116082 116082 38712
Volume Flow cuft/hr 10637 144 643 67820 28 1968 1968 276220
Enthalpy MMBtu/hr 0.985 -26.307 -26.307 -23.732 -33.665 -50.65 -50.65 -50.65
Mass Flow lb/hr
THF 594.758 5453.38 5453.38 5453.38 110277.9 110277.9 110277.9 36781.756
MAH
BUTANE 0.276 1.459 1.459 1.459 24.983
OXYGEN
N2
CO
CO2 2.479 0.554 0.554 0.554 2.739
WATER 32.876 2802.56 2802.56 2802.56 5688.02 5688.02 5688.018 1900.213
MA
FORMIC <0.001 0.046 0.046 0.046 <0.001
ACRYLIC 0.015 18.447 18.447 18.447 TRACE
H2 1309.32 1.818 1.818 1.818 1.88
BUTANOL 0.746 124.771 124.771 124.771 0.027
PROPANOL 0.014 0.934 0.934 0.934 0.006
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF 0.306 0.649 0.649 0.649 0.95 0.95 0.95 0.95
MAH
BUTANE 142 PPM 174PPM 174PPM 174PPM 645PPM 645PPM 645 PPM 645 PPM
OXYGEN
N2
CO
CO2 0.001 66 PPM 66 PPM 66 PPM 71 PPM 71 PPM 71 PPM 71 PPM
WATER 0.017 0.333 0.333 0.333 0.049 0.049 0.049 0.049
MA
FORMIC 134 PPB 5 PPM 5 PPM 5 PPM TRACE TRACE TRACE TRACE
ACRYLIC 8 PPM 0.002 0.002 0.002 TRACE TRACE TRACE TRACE
H2 0.675 216PPM 216PPM 216PPM 49 PPM 49 PPM 49 PPM 49 PPM
BUTANOL 384 PPM 0.015 0.015 0.015 706 PPB 706 PPB 706 PPB 706 PPB
PROPANOL 7 PPM 111PPM 111PPM 11 PPM 165 PPB 165 PPB 165 PPB 165 PPB
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
16
Stream No. 57 58 59 60 61 62 63 64
Temperature °F 151 174 174 174 241 328 291 284
Pressure psia 13.5 12.0 13.5 14.5 43.5 117.5 116.0 114.5
Vapor Frac 0.50 0.91 0 0 1 1 0.55 0.23
Mole Flow lbmol/hr 1637 1637 155 155 617 617 2272 2272
Mass Flow lb/hr 74701 74701 3058 3058 38712 38712 152630 152630
Volume Flow cuft/hr 1266 1266 53 53 106681 44387 2588 2588
Enthalpy MMBtu/hr -633.94 -346.34 -18.742 -18.742 -49.452 -48.214 -25.828 -45.218
Mass Flow lb/hr
THF 54337.4 54337.4 207.735 207.735 36781.76 36781.76 144235.8 144235.8
MAH
BUTANE 0.001 0.001 24.983 24.983
OXYGEN
N2
CO
CO2 TRACE TRACE 2.739 2.739
WATER 14388.3 14388.3 2705.84 2705.84 1900.213 1900.213 8242.045 8242.045
MA
FORMIC 0.046 0.046 <0.001 <0.001
ACRYLIC 65.5628 65.5628 18.447 18.447 TRACE TRACE
H2 TRACE TRACE 1.88 1.88
BUTANOL 5861.76 5861.76 124.744 124.744 0.027 0.027
PROPANOL
47.7289
8
47.7289
8 0.931 0.931 0.006 0.006
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF 0.727 0.727 0.068 0.068 0.95 0.95 0.945 0.945
MAH
BUTANE 311PPB 311PPB 345 PPM 645 PPM 710 PPM 710 PPM
OXYGEN
N2
CO
CO2 TRACE TRACE 71 PPM 71 PPM 78 PPM 78 PPM
WATER 0.193 0.193 0.885 0.885 0.049 0.049 0.054 0.054
MA
FORMIC 15 PPM 15 PPM TRACE TRACE TRACE TRACE
ACRYLIC 0.001 0.001 0.006 0.006 TRACE TRACE TRACE TRACE
H2 TRACE TRACE 49 PPM 49 PPM 53 PPM 53 PPM
BUTANOL 0.078 0.078 0.041 0.041 706 PPB 706 PPB TRACE TRACE
PROPANOL 0.001 0.001 304PPM 304PPM 165 PPB 165 PPB 93 PPB 93 PPB
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
17
Stream No. 65 66 67 68 69 70 71 72
Temperature °F 284 284 298 298 298 298 151 96
Pressure psia 114.5 116.0 114.0 112.5 114.0 116.0 14.7 14.7
Vapor Frac 0.23 1 0.49 0.97 0.00 0.00 0.45 0.00
Mole Flow lbmol/hr 2272 568 1772 1772 49 49 49 49
Mass Flow lb/hr 152630 35185 127779 127779 3526 3526 3526 3526
Volume Flow cuft/hr 2588 39054 2166 2166 78 78 9838 65
Enthalpy MMBtu/hr -45.218 -45.218 -555.774 -281.775 -4.147 -4.147 -4.147 -4.516
Mass Flow lb/hr
THF 144235.8 33255.34 127779.4 127779.4 3526.421 3526.421 3526.421 3526.421
MAH
BUTANE 24.983 TRACE TRACE TRACE TRACE
OXYGEN
N2
CO
CO2 2.739 TRACE TRACE TRACE TRACE
WATER 8242.045 1900.213 TRACE TRACE TRACE TRACE
MA
FORMIC TRACE <0.001 <0.001 <0.001 <0.001
ACRYLIC TRACE TRACE TRACE TRACE TRACE
H2 1.88 TRACE TRACE TRACE TRACE
BUTANOL 0.027 0.027 0.027 0.027
PROPANOL 0.003 0.003 0.003 0.003 0.003
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF 0.945 0.945 1 1 1 1 1 1
MAH
BUTANE 710 PPM 710 PPM TRACE TRACE TRACE TRACE
OXYGEN
N2
CO
CO2 78 PPM 78 PPM TRACE TRACE TRACE TRACE
WATER 0.054 0.054 TRACE TRACE TRACE TRACE
MA
FORMIC TRACE TRACE 9 PPB 9 PPB 9 PPB 9 PPB
ACRYLIC TRACE TRACE TRACE TRACE TRACE TRACE
H2 53 PPM 53 PPM TRACE TRACE TRACE TRACE
BUTANOL TRACE TRACE 8 PPM 8 PPM 8 PPM 8 PPM
PROPANOL 93 PPB 93 PPB 886 PPB 886 PPB 886 PPB 886 PPB
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
18
Stream No. 73 74 75 76 77 78
Temperature °F 284 284 284 113 113 113
Pressure psia 116.0 116.0 16.0 14.5 14.5 14.5
Vapor Frac 1.00 1.00 1.00 0.00 1.00 0.00
Mole Flow lbmol/hr 28 540 540 540 2 538
Mass Flow lb/hr 1759 33426 33426 33426 60 33365
Volume Flow cuft/hr 1953 37102 269831 1358 751 608
Enthalpy MMBtu/hr -2.261 -42.957 -42.957 -52.462 -0.076 -52.387
Mass Flow lb/hr
THF 1662.767 31592.57 31592.57 31592.57 55.753 31536.108
MAH
BUTANE 1.249 23.734 23.734 23.734 0.197 23.526
OXYGEN
N2
CO
CO2 0.137 2.602 2.602 2.602 0.418 2.185
WATER 95.011 1805.202 1805.202 1805.202 2.346 1803.493
MA
FORMIC TRACE TRACE TRACE TRACE TRACE TRACE
ACRYLIC TRACE TRACE TRACE TRACE
H2 0.094 1.786 1.786 1.786 1.724 0.062
BUTANOL TRACE <0.001 <0.001 <0.001 TRACE <0.001
PROPANOL <0.001 0.003 0.003 0.003 TRACE 0.003
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
Mass Frac
THF 0.945 0.945 0.945 0.945 0.922 0.945
MAH
BUTANE 710 PPM 710 PPM 710 PPM 710 PPM 0.003 705 PPM
OXYGEN
N2
CO
CO2 78 PPM 78 PPM 78 PPM 78 PPM 0.007 65 PPM
WATER 0.054 0.054 0.054 0.054 0.039 0.054
MA
FORMIC TRACE TRACE TRACE TRACE TRACE TRACE
ACRYLIC TRACE TRACE TRACE TRACE
H2 53 PPM 53 PPM 53 PPM 53 PPM 0.029 2 PPM
BUTANOL TRACE TRACE TRACE TRACE TRACE TRACE
PROPANOL 93 PPM 93 PPM 93 PPM 93 PPM 17 PPM 91 PPB
METHANOL
GAMMA-01
1:4-B-01
METHANE
PROPANE
SUCCI-02
19
Results
Based on our Aspen simulation we have created a standard PFD for your process. Again the
process was broken up into two pieces, the first ending with the production of maleic anhydride
and the second converting the maleic anhydride to tetrahydrofuran.
The selectivities generated in the Aspen simulation were different from the values found in
patent no. 4,317,778. This is probably due to thermodynamic model limitation. Multiple models
were evaluated an each gave the selectivity results. The process simulation values are shown
below.
Maleic Anhydride 82.3%
Carbon Monoxide 14.6%
Acrylic Acid 2.6%
Formic Acid 0.5%
The final process flow diagram is presented along with the equipment summary and economic
analysis. These can be found on the proceeding pages.
20
Equipment Summary
The following tables present the equipment summary for the entirety of the process of the
production of tetrahydrofuran from n-butane with maleic anhydride as the reaction intermediate.
Each piece of equipment is specifically sized based upon information taken from the attached
Aspen Plus Simulation, and heuristics found in Chapter 11 of Analysis, Synthesis and Design of
Chemical Processes. There are several key portions of the equipment summary to take note of,
which will be discussed in more detail below.
1. Certain pieces of equipment are either 316 SS plated, or their primary material of
construction is 316 SS.
Equipment such as pumps, heat exchangers, compressors, and towers that are 316
SS plated have been manufactured this way because they come into contact with
maleic anhydride or maleic acid.
Maleic anhydride and maleic acid are extremely corrosive to carbon steel, and
thus any equipment manufactured with carbon steel that comes in contact with
these chemicals will become a severe process safety hazard.
Equipment such as fired heaters and reactors are completely constructed of 316
SS. This is due to the large amount of heat and high temperatures that these
pieces of equipment must withstand. Weaker materials such as carbon steel will
not be able to hold up under these conditions and will eventually become a severe
process safety hazard.
2. Certain heat exchangers are floating head heat exchangers, while others are double pipe
heat exchangers.
Most heat exchangers in this process require a large heat transfer area due to the
large heat duties. Floating head heat exchangers, while more expensive than
double pipe heat exchangers, can accommodate this large area.
When possible, double pipe heat exchangers are used when the heat transfer area
is small enough.
3. All distillation towers and vertical vessels are priced with demisters included in the cost.
4. All trays in distillation towers are valve type trays. This decision was made to reduce the
cost of the distillation towers, as valve trays are less expensive than sieve trays.
5. More detailed explanations of equipment sizing calculations can be found in Appendix A.
21
Table 2. Equipment Summary.
Compressors and Drives
C-101 A/B C-201 A/B
Carbon Steel 316 SS
Centrifugal Centrifugal
Power =2408 hp Power = 271 hp
72% Efficiency 72% Efficiency
C-202 A/B C-203 A/B
Carbon Steel Carbon Steel
Centrifugal Centrifugal
Power = 554 hp Power = 573 hp
72% Efficiency 72% Efficiency
Fired Heaters
H-101 H-102
Required heat load = 3,150,000 btu/hr Required heat load = 9,610,000 btu/hr
Tubes = Stainless Steel Tubes = Stainless Steel
80% thermal efficiency 80% thermal efficiency
Maximum pressure rating of 40 psi Maximum pressure rating of 40 psi
H-103
Required heat load = 16,300,000 btu/hr
Tubes = Stainless Steel
80% thermal efficiency
Maximum pressure rating of 30 psi
Heat Exchangers
E-101 E-102
A = 1229 ft2 A = 207 ft
2
1-2 exchanger, floating head, carbon steel 1-2 exchanger, floating head, 316 SS Plated
Q = 4,330,000 btu/hr Q = -6,370,000 btu/hr
Maximum pressure rating of 15 psi Maximum pressure rating of 40 psi
E-103 E-104
A = 11846 ft2 A =1782 ft
2
1-2 exchanger, floating head, 316 SS Plated 1-2 exchanger, floating head, 316 SS Plated
Q = 12,800,000 btu/hr Q = -29,000,000 btu/hr
Maximum pressure rating of 40 psi Maximum pressure rating of 35 psi
E-105 E-106
A = 93 ft2 A = 5854 ft
2
1-2 exchanger, double pipe, 316 SS Plated 1-2 exchanger, floating head, 316 SS Plated
Q = -1,540,000 btu/hr Q = 2,890,000 btu/hr
Maximum pressure rating of 30 psi Maximum pressure rating of 30 psi
22
Heat Exchangers (Continued)
E-107 E-201
A = 3633.2 ft2 A = 1964 ft
2
1-2 exchanger, floating head, 316 SS Plated 1-2 exchanger, floating head, carbon steel
Q = -1,570,000 btu/hr Q = 1,170,000 btu/hr
Maximum pressure rating of 30 psi Maximum pressure rating of 615 psi
E-202 E-203
A = 190 ft2 A = 408 ft
2
1-2 exchanger, floating head, 316 SS Plated 1-2 exchanger, floating head, carbon steel
Q = 59,000 btu/hr Q = -6,980,000 btu/hr
Maximum pressure rating of 615 psi Maximum pressure rating of 365 psi
E-204 E-205
A = 2282 ft2 A = 743 ft
2
1-2 exchanger, floating head, carbon steel 1-2 exchanger, floating head, carbon steel
Q = 1,130,000 btu/hr Q = 2,580,000 btu/hr
Maximum pressure rating of 615 psi Maximum pressure rating of 15 psi
E-206 E-207
A = 7281 ft2 A = 2271 ft
2
1-2 exchanger, floating head, carbon steel 1-2 exchanger, floating head, carbon steel
Q = 23,700,000 btu/hr Q = -17,000,000 btu/hr
Maximum pressure rating of 15 psi Maximum pressure rating of 15 psi
E-208 E-209
A = 9777 ft2 A = 672 ft
2
1-2 exchanger, floating head, carbon steel 1-2 exchanger, floating head, carbon steel
Q = 18,600,000 btu/hr Q = -19,400,000 btu/hr
Maximum pressure rating of 120 psi Maximum pressure rating of 120 psi
E-210 E-211
A = 1079 ft2 A = 104 ft
2
1-2 exchanger, floating head, carbon steel 1-2 exchanger, floating head, carbon steel
Q = -8,470,000 btu/hr Q = -370,000 btu/hr
Maximum pressure rating of 15 psi Maximum pressure rating of 15 psi
Reactors
R-101 R-201
Stainless Steel, V5P6O50 Catalyst Stainless Steel, CuO/ZnO/Al2O3/Cr2O3 Catalyst
V = 1400 ft3 V = 42 ft
3
Maximum Pressure Rating of 40 psi Maximum Pressure Rating of 610 psi
Maximum catalyst temperature of 1030 oF Maximum catalyst temperature of 700
oF
23
Pumps
P-101 A/B P-102 A/B
Centrifugal/Electric drive Centrifugal/Electric drive
Carbon Steel Carbon Steel
Actual power = 0.443 hp Actual power = 0.13 hp
Efficiency 85% Efficiency 85%
P-103 A/B P-104 A/B
Centrifugal/Electric drive Centrifugal/Electric drive
316 SS 316 SS
Actual power = 0.233 hp Actual power = 0.603 hp
Efficiency 85% Efficiency 85%
P-105 A/B P-106 A/B
Centrifugal/Electric drive Centrifugal/Electric drive
316 SS 316 SS
Actual power = 0..434 hp Actual power = 0.04 hp
Efficiency 85% Efficiency 85%
P-107 A/B P-201 A/B
Centrifugal/Electric drive Centrifugal/Electric drive
316 SS Stainless steel
Actual power = 0.0.334 hp Actual power = 2.81 hp
Efficiency 85% Efficiency 85%
P-202 A/B P-203 A/B
Centrifugal/Electric drive Centrifugal/Electric drive
Carbon Steel Carbon Steel
Actual power = 1.8 hp Actual power = 3.1 hp
Efficiency 85% Efficiency 85%
P-204 A/B
Centrifugal/Electric drive
Carbon Steel
Actual power = 0.2.41 hp
Efficiency 85%
Towers
T-101 T-102
Stainless Steel Clad Stainless Steel Clad
3 SS sieve trays plus reboiler and condenser 30 SS sieve trays plus reboiler and condenser
70% efficient trays 70% efficient trays
Additional feed ports on tray 3 Reflux ratio 0.06
24-in tray spacing 24-in tray spacing
Column height 7 ft Column height 70 ft
Diameter 0.3 ft Diameter 3 ft
Maximum Pressure Rating 35 psi Maximum Pressure Rating 35 psi
24
Towers (Continued)
T-103 T-201
Stainless Steel Clad Carbon Steel
30 SS sieve trays plus reboiler and condenser 10 CS sieve trays plus reboiler and condenser
70% efficient trays 70% efficient trays
Reflux ratio 0.104 Reflux ratio 2
24-in tray spacing 24-in tray spacing
Column height 70 ft Column height 23 ft
Diameter 3 ft Diameter 1 ft
Maximum Pressure Rating 35 psi Maximum Pressure Rating 35 psi
T-202
Carbon Steel
20 CS sieve trays plus reboiler and condenser
70% efficient trays
Reflux ratio 3
24-in tray spacing
Column height 47 ft
Diameter 2 ft
Maximum Pressure Rating 35 psi
Vessels
V-101 V-102
Horizontal Horizontal
316 SS Clad 316 SS Clad
L/D=3 L/D=4
Volume=75 ft3 Volume=5 ft
3
V-201 V-202
Vertical Horizontal
Carbon Steel Carbon Steel
L/D=3 L/D=3
Volume=1955 ft3 Volume=350 ft
3
V-203
Horizontal
Carbon Steel
L/D=3
Volume=380 ft3
25
Capital and Manufacturing Costs
The economic analysis of this process was completed with the goal of finding the net present
value of the project after 10 years of operation. The cost of land for the facility is estimated at
$455,000.10
CAPCOST was used for the bare module cost of the equipment needed. The bare
module total was then scaled to the total module cost by multiplying by a factor of 1.18. The
total module cost could then be scaled to the desired grassroots cost by adding a grassroots factor
of .5 times the bare module cost. This lead to a grassroots cost, and therefore fixed capital
investment, of approximately $54,936,336.00. It is assumed that 60% of the FCI will be spent in
year 1 of construction and the other 40% will be spent in year 2. There are 33 non-particulate
processing steps in the process meaning 17 operators will be needed. At an approximate salary
of $52,900 per year, the cost of labor will be $899,300.00. Chemical costs were found from
several sources and the prices are summarized in Table 3 below. For the oxygen needed in this
process, air will be pumped in and therefore oxygen did not have a cost associated with it. Also,
there is a catalyst present in Reactor R-101 that was not considered in the raw material.
Table 3. Chemical Pricing
Component Price per lb
N-butane $ 0.33
Water $ 0.00003
Hydrogen $ 2.66
Oxygen $ -
Tetrahydrofuran $ 1.55 References 2,6, 9, 15
Using the prices from the table above, the raw material costs for this process are about
$36,103,813.05. The calculation of utilities has already been explained and results in a yearly
utility cost of $6,804,298.76. The only other cost needed to calculate the yearly cost of
manufacture is the cost of waste treatment. The majority of the waste streams in the process are
inert gases. These will be sent to a flare and burned. It was assumed that there is not a gas
associated with this. Two of the waste water streams were greater than 99% pure water. For this
reason, primary waste water treatment was priced for these streams. A third waste water stream
contained enough contaminates that it was assumed secondary waste water treatment would be
needed. The total for waste treatment came to $5,400 per year. Using all of above values, the
cost of manufacture without deprecation is approximately $65,127,254.50 per year.
A standard MACRS deprecation schedule was used starting in year 3. Tax is approximated at
40% based on a net taxable income of over $18 million and an interest rate of 10% p.a.19
It was
also assumed that the salvage value would be zero at the end of this process lifetime.
26
Table 4 below is an overall summary of the economic analysis of the base case design for this
process. All calculations are shown in Appendix A. The grassroots cost of this facility will be
approximately $54,936,336.00. The land will cost $455,000. Working capital for this project is
assumed to be 10% of the fixed capital investment which is $5,493,633.60. There will not be
salvage at the end of this project. Tax is assumed to be 40% and the interested rate used is 10%.
The net present value of this project, after 2 years of construction and 10 years of operation is
-$67,659,173.42. Assuming the 10% interest rate, it would be more profitable to invest the
grassroots cost than it would be to build this facility. Figures 3-6, show the after tax cash flow,
cumulative cash flow, discounted cash flow, and discounted cumulative cash flow respectively.
27
Table 4. Economic Analysis (in millions of dollars).
End of
Year Investment dk R COMd
After Tax
Profit
After Tax
Cash Flow
Cumulative
Cash Flow
Discounted
Cash Flow
Discounted
Cumulative Cash Flow
0.00 (0.46) 0.00 0.00 0.00 0.00 (0.46) (0.46) (0.46) (0.46)
1.00 (32.96) 0.00 0.00 0.00 0.00 (32.96) (32.96) (29.97) (30.42)
2.00 (27.47) 0.00 0.00 0.00 0.00 (27.47) (27.47) (22.70) (53.12)
3.00 0.00 10.99 47.60 65.13 (11.41) (0.42) (27.89) (0.31) (53.44)
4.00 0.00 17.58 47.60 65.13 (14.04) 3.54 (24.35) 2.42 (51.02)
5.00 0.00 10.55 47.60 65.13 (11.23) (0.68) (25.03) (0.42) (51.44)
6.00 0.00 6.33 47.60 65.13 (9.54) (3.21) (28.25) (1.81) (53.26)
7.00 0.00 6.33 47.60 65.13 (9.54) (3.21) (31.46) (1.65) (54.91)
8.00 0.00 3.16 47.60 65.13 (8.28) (5.11) (36.57) (2.38) (57.29)
9.00 0.00 0.00 47.60 65.13 (7.01) (7.01) (43.58) (2.97) (60.26)
10.00 0.00 0.00 47.60 65.13 (7.01) (7.01) (50.59) (2.70) (62.97)
11.00 0.00 0.00 47.60 65.13 (7.01) (7.01) (57.60) (2.46) (65.43)
12.00 5.95 0.00 47.60 65.13 (7.01) (7.01) (64.62) (2.23) (67.66)
28
Figure 3. Base case after tax cash flow (in millions of dollars).
Figure 4. Base case cumulative cash flow (in millions of dollars).
(35,000,000.00)
(30,000,000.00)
(25,000,000.00)
(20,000,000.00)
(15,000,000.00)
(10,000,000.00)
(5,000,000.00)
0.00
5,000,000.00
10,000,000.00
1 2 3 4 5 6 7 8 9 10 11 12 13
(70,000,000.00)
(60,000,000.00)
(50,000,000.00)
(40,000,000.00)
(30,000,000.00)
(20,000,000.00)
(10,000,000.00)
0.00
1 2 3 4 5 6 7 8 9 10 11 12 13 14
29
Figure 5. Base case discounted cash flow (in millions of dollars).
Figure 6. Base case discounted cumulative cash flow (in millions of dollars).
(35,000,000.00)
(30,000,000.00)
(25,000,000.00)
(20,000,000.00)
(15,000,000.00)
(10,000,000.00)
(5,000,000.00)
0.00
5,000,000.00
1 2 3 4 5 6 7 8 9 10 11 12 13
(80,000,000.00)
(70,000,000.00)
(60,000,000.00)
(50,000,000.00)
(40,000,000.00)
(30,000,000.00)
(20,000,000.00)
(10,000,000.00)
0.00
1 2 3 4 5 6 7 8 9 10 11 12 13
30
Optimization
After inspection of the waste streams surrounding the pressure swing distillation columns it was
decided that it was worthwhile economically to attempt to recover some of the THF that is sent
to waste. The main sources of waste were the top of the flash vessel in the recycle, the purge
stream, and the bottoms of the first tower.
It was decided to eliminate the flash vessel and add a small distillation column to purify some of
the THF in the purge stream. This column was designed with a similar temperature and pressure
of the second tower in the pressure swing. This helps to eliminate the need to heat exchangers
and pressure changers. The original towers were optimized by adjusting the reflux ratios and the
reboiler/condenser conditions. This eliminated most of the THF out of the bottoms of the first
and increased the mass flow of THF out of the second bottoms stream. A list of the streams that
exit the pressure swing system in the two scenarios are in the following charts. They show the
increase in product given the same initial feed.
31
Figure 7. Optimization simulation.
52
5954
53
57
58
60
56
63 64 65
55
61
62
T-201
S-202
T-202
CV-203 E-211
C-202
C-203
CV-204
T-203
32
Table 5. Purge stream flow rates before optimization.
Stream # 60 72 73 77
Description Waste Product Waste Waste
Bottoms T-201 Bottoms T-202 Purge Top V-204
THF
(lb/hr) 207.74 3526.42 1662.77 55.75
Waste = 1926.25
Product = 3526.42073
Table 6. Purge stream flow rates after optimization.
Stream # 53 65 61 62
Description Waste Product Waste Product
Bottoms T-201 Bottoms T-202 Distillate T-203 Bottoms T-203
THF
(lb/hr) 0.0049 4169.68 742.87 514.37
Waste = 742.88
Product = 4169.68
This optimization adds another operator to work the additional distillation column per shift, and
the capital cost of buying the tower. It also lowered the capital cost of the other two towers and
increased the product flow. The following chart summarizes the changes in the various cost and
increased revenue. It was decided that the optimization would ultimately increase our future net
value versus the base case design.
Table 7. Base case costs vs optimized costs.
Base Case Optimized
FCI $ 54,936,336.00 $ 46,174,094.40
CUT $ 6,804,298.76 $ 9,445,033.20
COL $ 899,300.00 $ 952,200.00
COMd $ 65,127,254.50 $ 66,988,807.65
CCP $ (64,615,384.39) $ (45,309,357.73)
NPV $ (67,659,173.42) $ (52,369,898.26)
Safety and Environmental
It is suggested that all personal wear appropriate clothing for protection. Long pants and steel
toed shoes are best. Also a hard hat, safety glasses, and ear plugs are strongly recommended.
33
Chemical Hazards
No part in this process is meant for human consumption and therefore should not be ingested by
any living creature. Many of the raw materials and products are toxic and potentially poisonous
if eaten. Another caution must be taken around exposing the streams to too much heat, flame, or
oxidizers.10
For the products that are present in the greatest quantities the National Fire Protection
Association values are included in Appendix C.
Process Hazards
The process is operated at the temperatures between 104°F and 500°F, and pressures between
14.5 psi and 145 psi, which will not cause severe processing difficulties and hazards, with the
exception of R-101 and R-201.
The first reactor, R-101, producing MAH operates at a high temperature. The reaction takes
place in the vapor phase, so the high temperature is required to maintain all species in the vapor
phase. Also, the selectivity and reaction rates are higher at high temperature. In R-201, the
reaction is operated at a high pressure. This is from the favorable equilibrium conversion and
increased reaction rate.
MAH is corrosive, maleic acid is harmful, and THF is flammable. The corrosion of the piping
and equipment over time may occur. Routine inspection should be practiced.
Extra care must be taken into providing proper containment, pressure reliefs, and temperature
control for the process.
Waste Treatment
This process has a large amount of waste streams. Conveniently, most of the waste streams are
vapor and inert gases with a small amount of unreacted material. All of these waste streams can
be burned to reduce the components to more environmentally friendly components. It may be
necessary to obtain EPA certifications on this exhaust but is a viable method of waste treatment
on these streams. There are 3 other waste streams that are composed mainly of water. The
distillate out of T-103 as well as the distillate out of T-102 are both over 99% water. For that
reason, they have been sent to a primary waste water treatment operation to filter these streams.
The bottoms of T-201 are about 84% water with a more significant amount of THF. It will be
sent through secondary waste water treatment. This includes filtration and processing through
activated sludge to clean up this waste water.
34
Conclusion
The optimization presented does not make the process profitable however it reduces the deficit.
We suggest that further optimization be explored before construction of the plant begins. After
the process is running fine tuning and final optimization may be determined. The main reason
this process is not profitable is because of the high cost of hydrogen. We suggest exploring more
profitable final products using Tetrahydrofuran.
35
References
1. Acrylic Acid: MSDS No. A1562 [Online]: Avantor Performance Materials, Inc.: Center
Valley, PA, Feb 28, 2011. http://www.avantormaterials.com/documents/MSDS/usa/
English/A1562_msds_us_Default.pdf (accessed Dec 02, 2011).
2. Amos, W.A.; Costs of Storing and Transporting Hydrogen; DE-AC36-83CH10093;
National Renewable Energy Laboratory, Golden, CO, 1998.
3. Blum, P. R.; Nicholas, M. L. Preparation of Maleic Anhydride Using Fluidized Catalysts.
U.S. Patent 4,317,778, Dec 29,1980.
4. Budge, J. R.; Attig, T. G. Vapor-phase Hyrdogenation of Maleic Anhydride to
Tetrahydrofuran and Gamma-butyrolactone. U.S. Patent 5,072,009, Dec 10, 1991.
5. Butane; MSDS No. 1807 [Online]: Hovensa LLC: Christainsted, VI, May 1, 2006.
http://www.hovensa.com/pdf/butane.pdf (accessed Dec 02, 2011)
6. CW Price Report. Chemical Week [Online] May 3, 2010; 172(10):69. Academic Search
Premier. http:/ http://web.ebscohost.com.proxy.mul.missouri.edu (accessed November 7,
2011).
7. Formic Acid; MSDS No. F5956 [Online]: Avantor Performance Materials, Inc.: Center
Valley, PA, Aug 24, 2011. http://www.avantormaterials.com/documents/MSDS/usa/
English/F5956_msds_us_Default.pdf (accessed Dec 02, 2011).
8. Hydrogen, compressed; MSDS No. 1009 [Online]: Air Products and Chemicals, Inc.:
Allentown, PA, June 1994. http://avogadro.chem.iastate.edu/MSDS/hydrogen.pdf
(accessed Dec 02, 2011).
9. ICIS. http://www.icis.com/chemicals/channel-info-chemicals-a-z/ (accessed Dec 03,
2011).
10. Land Watch. http://www.landwatch.com/Pike-County-Missouri-Land-for-sale/ pid/
146300329 (accessed Dec 03, 2011).
11. Lewis, R. J., Sr. Hazardous Chemicals Desk Reference, 5th
ed.; John Wiley & Sons, Inc.:
New York, 2002; pp 24-1132.
12. Luyben, W.L,; Chien, I.L. Pressure-Swing Azeotropic Distillation. Design and Control of
Distillation Systems for Separating Azeotropes; John Wiley & Sons, Inc.: New Jersey, pp
149-162.
13. Maleic Acid; MSDS No. M0325 [Online]: Avantor Performance Materials, Inc.: Center
Valley, PA, March 08, 2011. http://www.avantormaterials.com/documents/MSDS/usa/
English/M0325_msds_us_Default.pdf (accessed Dec 02,2011).
14. Maleic Anhydride; MSDS No. M0364 [Online]: Avantor Performance Materials, Inc.:
Center Valley, PA, March 03, 2011. http://www.avantormaterials.com/documents/
MSDS/usa/English/M0364_msds_us_Default.pdf (accessed Dec 02 2011).
15. Matheson Home Page. http://www.mathesongas.com (accessed Nov 10, 2011).
16. n-Butyl Alcohol; MSDS No. B5860 [Online]: Avantor Performance Materials, Inc.:
Center Valley, PA, Aug 26, 2011. http://www.avantormaterials.com/documents/MSDS/
usa/English/B5860_msds_us_cov_Default.pdf (accessed Dec 02, 2011).
36
17. Ninagawa, S. Recovery of Maleic Acid from its Gaseous Mixtures with Acetic Acid. U.S.
Patent 3,624,148, Nov 30, 1971.
18. Tetrahydrofuran; MSDS No. T1222 [Online]: Avantor Performance Materials, Inc.:
Center Valley, PA, Aug 30, 2011. http://www.avantormaterials.com/documents/MSDS/
usa/English/T1222_msds_us_cov_Default.pdf (accessed Dec 02, 2011).
19. Turton, R.; Bailie, R.; et. al. Analysis, Synthesis, and Design of Chemical Processes;
Pearson Education: Boston, 2009; pp 5-1043.
20. Slinkard, W. E.; Baylis, A. B. Vapor Phase Oxidation of Butane Producing Maleic
Anhydride and Acetic Acid. U.S. Patent 4,052,417, Nov 6, 1975.
37
Appendix A – Sample Calculations
Mass and Energy Balances
Overall
An inspection of all the mass flowing into and out of the system was performed to ensure that the
process did not break the law of conservation of mass. The following charts show that the
system does indeed preserve this law.
(11)
Table A.1. Mass flow of input streams.
Stream # 1 2 10 39 SUM
Component Mass Flow lb/hr
Water 0.00 495.20 30887.20 858.23 32240.63
Butane 5500.45 0.00 0.00 0.00 5500.45
Oxygen 0.00 19754.40 0.00 0.00 19754.40
CO2 0.00 50.33 0.00 0.00 50.33
N2 0.00 64436.36 0.00 0.00 64436.36
Total 121982 lb/hr
38
Table A.2. Mass flow of output streams.
Stream # 13 22 33 46 60 72 73
Component Mass Flow lb/hr
Water 10623.85 26278.65 1495.87 1.73 2705.84 0.00 95.01
Butane 4.89 0.63 0.00 0.01 0.00 0.00 1.25
Oxygen 8238.82 6.38 0.00 0.00 0.00 0.00 0.00
MAH 0.00 0.54 0.00 0.00 0.00 0.00 0.00
CO 775.15 8.27 0.00 0.13 0.00 0.00 0.00
CO2 1427.22 18.21 0.00 0.00 0.00 0.00 0.14
Formic 0.79 147.70 1.15 0.00 0.05 0.00 0.00
Acrylic 3.66 42.40 7.81 0.00 18.45 0.00 0.00
N2 64393.97 0.02 0.00 0.00 0.00 0.00 0.00
THF 0.00 0.00 0.00 31.31 207.74 3526.42 1662.77
Butanol 0.00 0.00 0.00 0.04 124.74 0.03 0.00
Propanol 0.00 0.00 0.00 0.00 0.93 0.00 0.00
Methanol 0.00 0.00 0.00 0.00 0.00 0.00 0.00
H2 0.00 0.00 0.00 68.91 0.00 0.00 0.09
Stream # 77 SUM
Component Mass Flow lb/hr
Water 2.35 41203.30
Butane 0.20 6.98
Oxygen 0.00 8245.20
MAH 0.00 0.54
CO 0.42 783.97
CO2 0.00 1445.57
Formic 0.00 149.69
Acrylic 0.00 72.32
N2 55.75 64449.74
THF 0.00 5428.23
Butanol 0.00 124.81
Propanol 0.00 0.93
Methanol 1.72 1.72
H2 0.00 69.01 Total 121982 lb/hr
An inspection of all the energy flowing into and out of the system was preformed to ensure that
the process did not break the law of conservation of energy. The energy values were found using
the aspen stream results and equipment results. The net energy show in the chart does equal zero
however. This can be explained by Aspen having pump and compressor efficiencies of around
85%. This energy loss accounts for the difference.
39
(12)
Table. A.3. Energy balance for the process.
Stream #
Energy
(MMBTU/hr) Source
Net Energy
(MMBTU/ hr)
IN Heat Exchangers 4.32
1 -6.00 Towers -9.31
2 -3.24 Reactors -62.12
10 -211.08 Pumps/Compressors 9.69
39 -0.02
SUM = -220.33 NET = -57.42
OUT
13 -66.25
22 -177.36
33 -9.96
46 -0.04
60 -18.74
72 -4.52
73 -2.26
77 -0.08
SUM = -279.21 NET = -1.45
40
Reboiler and Reflux Streams
T-102
Table A.4. T-102 data from Aspen Plus.
Stage Temp Press.
Heat
duty
Liquid
enthalpy
Vapor
enthalpy Liquid Vapor Liquid Vapor
F psia
MMBt
u/hr
MMBtu
lbmol
MMBtu
lbmol
lbmol/
hr
lbmol/
hr lb/hr lb/hr
1 164.6 29.01 -28.99 -0.12 -0.02 1550.9 0.00 28093 0.00
2 248.5 29.01 0.00 -0.12 -0.10 91.03 1550.9 1652.6 28093.0
… … … … … … … … …
29 259.7 29.01 0.00 -0.16 -0.10 671.84 698.96 24332 13140
30 447.7 29.01 12.80 -0.30 -0.11 83.52 588.32 9152.8 15179.3
Table A.5. T-102 mass fractopm data from Aspen Plus.
Stage WATER BUTANE OXYGEN CO CO2 FORMIC ACRYLIC N2 MA
30 0.400 0.000 0.000 0.000 0.000 0.003 0.038 0.000 0.559
Stream 18
T18 = Tstage 2
18
(13)
(14)
Total mass flow from stage 1
Total mole flow from stage 1
(15)
(16)
Mass fractions same as stream 22
(17)
Stream 19
T19 = Tstage 1
18
(18)
41
(19)
Total mass flow from stage 1
Total mole flow from stage 1
Volumetric flow rate, see stream 18
Enthalpy same as stream 22
Stream 20
Same as stream 19
Stream 21
Same as 22 expect mass, mole, and volumetric flow rate
Mass, mole, and volumetric flow rate, see stream 18
Stream 23
T23 = Tstage 29
(20)
(21)
Total mass flow from stage 30
Total mole flow from stage 30
Volumetric flow, see stream 18
( ) ( )
( )
(22)
Mass fraction determined form Aspen Plus, stream 30.
Stream 24
T24 = Tstage 30
18
(23)
(24)
Total mass flow from stage 30
Total mole flow from stage 30
Volumetric flow, see stream 18
42
( ) ( )
( )
(25)
Mass fraction same as 23
Stream 25
T25 = T26
18
(26)
Composition and flow rates are the same at stream 26
Heat Integration
In this process, there are a total of 10 process streams that require heating or cooling. These are
listed in Table A.6.
Table A.6. Heat exchange stream data.
Stream Condition Tin (°F) Tout (°F) Qavailable
(BTU/hr)
8 Hot 770 203 15600633
26 Hot 447.7 104 1533989
43 Hot 464 104 6980495
75 Hot 236.3 113 9505120
71 Hot 150.8 96 369413
11 Cold 58.8 203 -4326818
40 Cold 70 464 -1167948
37 Cold 444.8 464 -71642
48 Cold 228.8 464 -1127207
51 Cold 102.9 176 -2575080
Total Q = 24720955
E m (lb/hr) Cp
(BTU/lb)
mCp
(BTU/(hr·°F))
E-102 90237 0.3049 27514
E-105 9153 0.4876 4463
E-203 10447 1.8561 19390
E-210 33426 2.3063 77089
E-211 3526 1.9116 6741
E-101 30887 0.9715 30006
E-201 858 3.4540 2964
E-202 7648 0.4879 3731
E-204 1941 2.4697 4793
E-205 8404 4.1917 35227
43
In Table A.6, the data of flow rate ṁ, Tin, Tout, Qavailable are obtained from the Aspen. Cp is
calculated using the following equation
( ) (27)
Using a minimum approach temperature is 10°F the Temperature Interval Diagram was
constructed.
44
Figure A.1. Temperature Interval Diagram.
Stream 8 26 43 75 71 11 40 37 48 51
mCp 27514.34 4463.16 19390.26 77089.38 6741.11 30005.67 2964.34 3731.35 4792.55 35226.81 (BTU/(hr·°F)) ∑mCpΔT
770 760 (BTU/hr)
A 8144245
474 464
B 160261
464 454
C 325831
454.8 444.8
D 277949
447.7 437.7
E 9219338
236.3 226.3
F 2923982
213 203
G 954871
203 193
H 1155537
186 176
I 1152658
150.8 140.8
J 1492612
113 103
K -21379
104 94
L -209831
96 86
M -816154
68.8 58.8
∑ 24759920
45
The small difference between the Qavailable and the in the Temperature Interval
Diagram is because the numbers in the EXCEL are rounded. was determined by the
sum of the individual streams in the section.
Section B:
( ) ( )
( ) ( )
(28)
Based on the Temperature Interval Diagram, we can construct the cascade diagram.
Figure A.2. Cascade diagram. All values are in Btu/hr.
46
There’s no pinch in this process, and we only need cold utilities. The load of the cold utilities is
Qc =24759920 Btu/hr.
The calculation of the minimum number of exchangers is shown in Figure A.3.
47
Figure A.3. Calculation of minimum number of exchangers. All values are in Btu/hr.
The Heat Exchanger Network is configured in Figure A.4. We can use hot stream 8 to heat stream 37, 48, 40, 11 and 51, and use the
cold utilities to cool stream 8, 26, 43, 75, 71. The load of each heat exchanger was calculated like the example of exchanger 1 below.
( ) ( )
(29)
48
Figure A.4. Design of Heat-Exchanger Network. All values are in Btu/hr.
49
Equipment Sizing
Heat Exchangers
Values for the temperature and pressure of high, medium, and low pressure steam, as well as
cooling water can be found in Table 8.3 of Analysis, Synthesis, and Design of Chemical
Processes.
Values for heat exchanger coefficients can be found in Table 11.11 of Analysis, Synthesis,
and Design of Chemical Processes.
The following is a sample calculation for the heat transfer area of heat exchanger E-101.
(30)
(31)
( ) ( )
( )
( )
(32)
(33)
The above values and equations - along with a heat duty (Q, BTU/hr) determined using the
Aspen Plus Simulation - provide the necessary information to find the heat transfer area of
the heat exchanger.
The temperature of the heating medium does not change; rather the heat transfer occurs due
to the heat of vaporization as steam condenses to water. The necessary steam flow rate and
price of the utility can be determined using the following equations and data taken from heat
exchanger E-101:
(34)
(35)
(36)
(37)
Similarly, the price can be determined using the necessary heat duty of the heat exchanger,
and the same price will be found.
(38)
50
(39)
Heat exchangers with a negative heat duty are sized in the exact same manner as an
exchanger with a positive heat duty. The only differences between the two are the heat
transfer coefficients in use for coolers. Water is used as a heating medium rather than steam,
and thus heat transfer occurs much more efficiently leading to generally smaller heat
exchange areas than are needed for positive heat duty exchangers.
(40)
(41)
( ) ( )
( )
( )
(42)
(43)
Process cooling water is produced at a temperature of 86 oF, and is heated to a maximum
temperature of 104 oF.
The necessary process cooling water flow rate and price of the utility can be determined
using the following equations and data taken from heat exchanger E-102:
(44)
( )
(45)
(46)
(47)
Similarly, the price can be determined using the necessary heat duty of the heat exchanger,
and the same price will be found.
(48)
(49)
Distillation Towers
The number of stages in each distillation tower is determined using Aspen Plus.
The tower height is determined using the spacing between each tray, which is a range
between 20 and 24 in. The maximum value of 24 in. has been chosen for sizing of trays in
this project.
51
The following is a sample calculation for distillation tower T-102:
(50)
(51)
The tower diameter is determined using a heuristic for the diameter based upon the ratio of
the tower length and diameter. This heuristic states that the ratio L/D must be less than 30,
and preferably less than 20 due to special design considerations for ratios above these values.
A value of L/D of 20 has been chosen for these calculations.
(52)
(53)
(54)
Finally, in order to determine the actual height of the tower, space must be made available for
the vapor disengagement as well as the reboiler return sections of the tower. The heuristic
for this calculation states that for a diameter of 3 feet, 4 feet must be added to the top for the
vapor disengagement and 6 feet must be added to the bottom for the reboiler return.
(55)
(56)
(57)
(58)
(59)
(60)
Therefore, T-102 has a total height of 70 ft and a diameter of 3ft.
Vessels
The following is a sample calculation for vessel V-101.
The volume of a vessel is determined using the volume of fluid to fill the vessel half-way for
a five minute period of time.
(61)
(62)
(63)
52
The dimensions of this vessel are then determined using an optimum ratio of the length and
the diameter, taken from Table 11.6 of Analysis, Synthesis and Design of Chemical
Processes.
(63)
(64)
(65)
√
(66)
√
(67)
(68)
(69)
Reactors
The necessary size of a reactor is entirely dependent upon the volumetric flowrate of the
process fluid as well as the residence time required to achieve the desired conversion of
reactants.
This information can be found on patents describing the specific reaction in question.
The following is a sample calculation for reactor R-201, which has a residence time of five
seconds.
(70)
(71)
Pumps and Compressors
Both pumps and compressors are sized using data taken directly from Aspen Plus.
We have chosen to use centrifugal pumps at an efficiency of 80% because all of the pumps
run at a volumetric flow rate greater than 500gpm (67 ft3/min). This efficiency value is found
in table 11.9 of Analysis, Synthesis and Design of Chemical Processes.
A sample calculation of the necessary utility cost to power a pump can be seen below for
pump P-201A/B:
(72)
(73)
Compressors are sized in the exact same manner using power data taken from Aspen Plus.
A sample calculation of the necessary utility cost to power a compressor can be seen below
for C-201A/B:
53
(74)
(45)
Fired Heaters
Fired heaters are sized using heat duty given from Aspen Plus, as well as heating rates for
various types of fired heaters found in Table 11.11 of Analysis, Synthesis, and Design of
Chemical Processes.
We have chosen to use radiant heaters due to their large heating rate of 12,000 BTU/hr/ft2.
The following is a sample calculation for fired heater H-101:
(76)
(77)
Fired heaters are powered by burning natural gas, and therefore do not fall under the same
utility category as steam for other heat exchangers. Therefore, there is a different method for
calculating the utility cost of a fired heater.
(78)
(79)
Notes
Heuristics for sizing each piece of equipment can be found in Chapter 11 of Analysis,
Synthesis and Design of Chemical Processes.
Each heuristic used is noted in the specific section of each piece of equipment, along with the
appropriate table where the heuristic can be found.
The cost of each specific utility is found in Table 8.3 of Analysis, Synthesis and Design of
Chemical Processes. A summary of each utility used can be found below in Table A.7.
Table A.7. Utility Costs.
Utility Cost
High Pressure Steam 18.67 $/MBTU
0.0136 $/lb
Cooling Water 0.0004 $/ft3
0.37 $/MBTU
Fuel oil 11.71 $/MBTU
Electricity 0.08 $/HP h
54
Capital and Manufacturing Costs
1. All equipment is priced using information determined while sizing such as:
a. Heat transfer area
b. Volume of vessels, towers, reactors
c. Fluid power of pumps and compressors
d. Number of trays for distillation towers
2. The following equation is used to determine the purchased cost of equipment:
( ) ( ) [ ( )]
(80)
a. is the purchased cost of the equipment in 2001.
b. Values for K1, K2 and K3 are found in Table A.1 of Appendix A of Analysis,
Synthesis and Design of Chemical Processes and are dependent upon the
equipment type and the specific equipment description.
c. A is the specific capacity of the equipment being priced.
3. must be converted into the price of the equipment in 2011. This is done using the
ratio of the 2011 value of the CEPCI (564.8) and the 2001 value of the CEPCI (397).
( )
( )
(81)
4. Once the value of is determined, it must be converted into the bare module cost, .
The bare module cost takes into account different materials of construction than carbon
steel, as well as any pressure factors that would lead to scale-up of the piece of
equipment. This is done using the scaling factor, .
(82)
a. Generally, the value of is as follows, but certain pieces of equipment use
different methods of calculating this factor, which will be explained in their
individual sections.
( ) (83)
b. B1 and B2 are found using Table A.4 of Appendix A of Analysis, Synthesis and
Design of Chemical Processes and are specific to the type of equipment being
priced.
55
c. FM is the materials factor which is found using Table A.3 and Figure A.18 of
Appendix A of Analysis, Synthesis and Design of Chemical Processes and are
specific to the type of equipment being priced.
d. FP is the pressure factor and is found using the following equation:
( ) ( ) [ ( )] (84)
e. Values of C1, C2 and C3 are found in Table A.2 of Appendix A of Analysis,
Synthesis and Design of Chemical Processes and are specific to the type of
equipment being priced.
f. P is pressure and is in units of barg for these calculations.
g. FP is not always necessary, only if the pressure inside the equipment is above a
certain pressure which is dependent upon the specific type of equipment being
sized.
5. Once the value of CBM is determined, the total module cost, CTM must be found. The
total module cost takes into account possible contingency and fee costs as well as
auxiliary facility costs. The total module cost is the sum of the individual bare module
costs multiplied by a scaling factor to account for the additional costs.
(85)
6. All values found for the above equations presented in Appendix A of Analysis, Synthesis
and Design of Chemical Processes are presented in SI units, and so each sample
calculation will be first converted to that system.
56
7. Heat Exchangers
The following is a sample calculation for a 316 stainless steel, floating head, and shell
and tube heat exchanger with a heat transfer area of 500 ft3 and a maximum pressure
of 100 psig.
o 500 ft2 = 46.5 m
2
o 100 psig = 6.9 barg
o K1 = 4.8306 K2 = -0.8509 K3 = 0.3187
o C1 = 0.03881 C2 = -0.11272 C3 = 0.08183
o B1 = 1.63 B2 = 1.66
o FM = 2.75
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(86)
( )
( )
(81)
( )
(87)
( ) ( ) [ ( )] (84)
( ) ( ) [ ( )] (88)
( ) (83)
( ) (89)
(82)
(90)
Therefore, from the above calculations, the bare module cost of this heat exchanger is
$175,540.30.
57
8. Distillation Towers
Towers and vessels use a special method to determine the pressure factor involved in
calculating the bare module cost. This equation is as follows:
( )
[ ( )]
(91)
o P is the maximum pressure in barg
o D is the diameter in m
Trays use a special method to determine the bare module cost. This equation is as
follows:
(92)
( ) ( ) ( ( )) (93)
(94)
o Fq is a quantity factor used only for trays
o N is the number of trays
The following is a sample calculation for a carbon steel tray tower with a total of 25
316 stainless steel valve trays, a volume of 750 ft3, a diameter of 5 ft and a maximum
pressure of 125 psig.
o 750 ft3 = 21.2 m
3
o 5 ft = 1.52 m
o A = 1.8 m2
o 125 psig = 8.62 barg
o Tower:
K1 = 3.4974 K2 = 0.4485 K3 = 0.1074
FM = 1
B1 = 2.25 B2 = 1.82
o Trays:
K1 = 3.3322 K2 = 0.4838 K3 = 0.3434
Fq = 1
FBM = 1.8
o Pricing of the tower:
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(95)
( )
( )
(81)
58
( )
(96)
( )
[ ( )]
(91)
( )
[ ( )]
(97)
( ) (83)
( ) (98)
(82)
(99)
o Pricing of the trays
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(100)
( )
( )
(81)
( )
(102)
(92)
(103)
o The total bare module cost for this piece of equipment is the sum of the bare
module costs of the tower as well as the trays.
(104)
(105)
Therefore, from the above calculations, the bare module cost of this distillation tower
is $347,419.37.
59
9. Vessels
Vessels are sized in a similar manner to distillation towers, with the same
modification to the pressure factor but without the addition of trays.
The following is a sample calculation for a horizontal, 316 stainless steel clad vessel
with a volume of 50 ft3 and a diameter of 3ft with a maximum pressure of 150 psig.
o 50 ft3 = 1.42 m
3
o 3 ft = 0.91 m
o 150 psig = 10.34 barg
o K1 = 3.5565 K2 = 0.3376 K3 = 0.0905
o FM = 1.65
o B1 = 1.49 B2 = 1.52
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(106)
( )
( )
(81)
( )
(107)
( )
[ ( )]
(91)
( )
[ ( )]
(108)
( ) (83)
( ) (109)
(82)
(110)
Therefore, from the above calculations, the bare module cost of the vessel is
$30,022.58.
60
10. Reactors
Reactor prices are based solely dependently upon the volume of the reactor. The bare
module factor is a constant value of 4 for each type of reactor.
The following is a sample calculation for a jacketed agitated reactor with a volume of
1000 ft3.
o 1000 ft3 = 28.3 m
3
o K1 = 4.1052 K2 = -0.4680 K3 = -0.0005
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(111)
( )
( )
(81)
( )
(112)
(82)
(114)
Therefore, from the above calculations, the bare module cost of the reactor is
$16,412.85.
61
11. Pumps
The following is a sample calculation for a 316 stainless steel, centrifugal, pump with
a shaft power of 50 hp and a discharge pressure of 250 psig.
o 50 hp = 37.3 kW
o 250 psig = 17.2 barg
o K1 = 3.3892 K2 = 0.0356 K3 = 0.1538
o C1 = -0.3935 C2 = 0.3957 C3 = -0.00226
o B1 = 1.89 B2 = 1.35
o FM = 2.6
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(115)
( )
( )
(81)
( )
(116)
( ) ( ) [ ( )] (84)
( ) ( ) [ ( )] (117)
( ) (83)
( ) (118)
(82)
(119)
Therefore, from the above calculations, the bare module cost of the pump is
$59,225.59. A spare pump is always purchased so that production will continue
during regularly scheduled pump maintenance or failure. This brings the total bare
module cost for the pump to $118,451.18.
62
12. Compressors
Compressors do not rely upon a variable bare module factor, rather the value is
constant for each type of compressor. The modification comes with the inclusion of a
drive that is priced separate from the compressor.
The following is a sample calculation for a carbon steel rotary compressor with a
fluid power of 250 hp and an explosion-proof electric motor.
o 250 hp = 184 kW
o Compressor
K1 = 5.0355 K2 = -1.8002 K3 = 0.8253
FBM = 2.4
o Drive
K1 = 2.4604 K2 = 1.4191 K3 = -0.1798
FBM = 1.55
o Pricing of the compressor:
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(120)
( )
( )
(81)
( )
(121)
(82)
(122)
o Pricing of the drive
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(123)
( )
( )
(81)
( )
(124)
(83)
(125)
The total bare module cost for this compressor is the sum of the bare module costs of
the compressor as well as the drive.
(126)
(127)
Therefore, from the above calculations, the bare module cost of the compressor is
$655,480.60. A spare compressor is always purchased so that production will
63
continue during regularly scheduled compressor maintenance or failure. This brings
the total bare module cost for the compressor to $1,310,961.20.
13. Fired Heaters
The following is a sample calculation for a stainless steel fired heater with a heat duty
of 170 MBTU/h and a maximum pressure of 600 psig.
o 170 MBTU/h = 49,822 kW
o 600 psig = 41.4 barg
o K1 = 7.3488 K2 = -1.1666 K3 = 0.2028
o C1 = 0.1347 C2 = -0.2368 C3 = 0.1021
o FBM = 2.8
o FT = 1
( ) ( ) [ ( )]
(80)
( ) ( ) [ ( )]
(128)
(129)
( )
( )
(81)
( )
(130)
( ) ( ) [ ( )] (84)
( ) ( ) [ ( )] (131)
(132)
(133)
Therefore, from the above calculations, the bare module cost of the fired heater is
$9,177,874.58.
64
1. Finding the Total Module Cost
The above sections give a sample of how to calculate each type of equipment that is
used in this process. Table A.8 below gives a summary of the price determined for
each piece of equipment at the current 2011 value.
Table A.8. Bare Module Cost Summary.
Equipment Price
Heat Exchanger $175,540.27
Distillation Tower $347,419.37
Vessel $30,022.58
Reactor $16,412.65
Pump $118,451.18
Compressor $1,310,961.20
Fired Heater $9,177,874.58
Sum $11,176,681.83
As can be seen above in Table A.8., the sum of the bare module costs for these pieces
of equipment is $11,176,681.83.
The final step in finding the total module cost is to factor for any possible extra fees.
(134)
(135)
65
Table A.9. CAPCOST program for the conversion of n-butane to maleic acid.
Compressors Compressor Type
Power
(kilowatts) # Spares MOC
Purchased
Equipment
Cost
Bare Module
Cost
C-101 Centrifugal 1800 1 CS $ 1,210,000 $ 3,310,000
Exchangers Exchanger Type
Shell
Pressure
(barg)
Tube
Pressure
(barg) MOC
Area
(square
meters)
Purchased
Equipment
Cost
Bare Module
Cost
E-101 Floating Head 1.03 1.03 CS / CS 114 $ 38,200 $ 126,000
E-102 Floating Head 2.76 2.76 SS / CS 19.2 $ 26,100 $ 121,000
E-103 Floating Head 2.76 2.76 SS / CS 1100 $ 222,000 $ 1,030,000
E-104 Floating Head 2.41 2.41 SS / CS 166 $ 46,300 $ 215,000
E-105 Double Pipe 2.41 SS / CS 8.64 $ 5,170 $ 23,500
E-106 Floating Head 2.07 2.07 SS / CS 544 $ 110,000 $ 509,000
E-107 Double Pipe 2.07 SS / CS 6.32 $ 4,870 $ 22,100
Fired
Heaters Type
Heat Duty
(MJ/h)
Steam
Superheat
(°C) MOC
Pressure
(barg)
Purchased
Equipment
Cost
Bare Module
Cost
H-101 Process Heater 3690 SS 2.76 $ 673,000 $ 1,890,000
H-102 Process Heater 10100 SS 2.76 $ 778,000 $ 2,190,000
H-103 Process Heater 17200 SS 2.76 $ 901,000 $ 2,530,000
66
Pumps
(with drives) Pump Type
Power
(kilowatts) # Spares MOC
Discharge
Pressure
(barg)
Purchased
Equipment
Cost
Bare Module
Cost
P-101 Centrifugal 0.33 1 CS 1.72 $ 6,970 $ 27,800
P-102 Centrifugal 0.095 1 CS 2.76 $ 6,970 $ 27,800
P-103 Centrifugal 0.45 1 SS 2.07 $ 6,970 $ 34,600
P-104 Centrifugal 0.45 1 SS 2.07 $ 6,970 $ 34,600
P-105 Centrifugal 0.324 1 SS 2.07 $ 6,970 $ 34,600
P-106 Centrifugal 0.031 1 SS 2.07 $ 6,970 $ 34,600
P-107 Centrifugal 0.249 1 SS 30 $ 6,970 $ 46,100
Reactors Type
Volume
(cubic
meters)
Purchased
Equipment
Cost
Bare Module
Cost
R-101 Jacketed Non-Agitated 39.6 $ 46,200 $ 69,300
Towers Tower Description
Height
(meters)
Diameter
(meters)
Tower
MOC
Demister
MOC
Pressure
(barg)
Purchased
Equipment
Cost
Bare Module
Cost
T-101 3 SS Valve Trays 1.68 0.914
Stainless
Clad SS 1.7 $ 14,400 $ 41,400
T-102 30 SS Valve Trays 16.8 0.396
Stainless
Clad SS 2.07 $ 77,200 $ 181,000
T-103 30 SS Valve Trays 16.8 0.183
Stainless
Clad SS 2.07 $ 127,000 $ 265,000
67
Vessels Orientation
Length/Heigh
t (meters) Diameter (meters) MOC
Demister
MOC
Pressure
(barg)
Purchased
Equipment Cost
Bare Module
Cost
V-101 Horizontal 2.9 0.975
Stainless
Clad 2.07 $ 7,020 $ 29,000
V-102 Horizontal 1.13 0.366
Stainless
Clad 2.07 $ 2,740 $ 11,300
Total Bare Module Cost $ 12,803,700
68
Figure A.10. CAPCOST program for the conversion of maleic anhydride to tetrahydrofuran.
Compressors Compressor Type
Power
(kilowatts) # Spares MOC
Purchased
Equipment
Cost
Bare Module
Cost
C-201 Rotary 202 1 SS $ 532,000 $ 2,680,000
C-202 Rotary 413 1 CS $ 2,680,000 $ 6,460,000
C-203 Rotary 427 1 CS $ 2,920,000 $ 7,040,000
Exchangers Exchanger Type
Shell
Pressure
(barg)
Tube
Pressure
(barg) MOC
Area
(square
meters)
Purchased
Equipment
Cost
Bare Module
Cost
E-201 Floating Head 42.4 42.4 CS / CS 157 $ 44,900 $ 161,000
E-202 Floating Head 42.7 42.7 SS / CS 17.7 $ 26,200 $ 136,000
E-203 Floating Head 25 25 CS / CS 37.9 $ 27,200 $ 94,000
E-204 Floating Head 42.7 42.7 CS / CS 212 $ 53,600 $ 192,000
E-205 Floating Head 1 1 CS / CS 69 $ 31,400 $ 103,000
E-206 Floating Head 2.07 2.07 CS / CS 676 $ 134,000 $ 442,000
E-207 Floating Head 2.07 2.07 CS / CS 211 $ 53,400 $ 176,000
E-208 Floating Head 8.62 8.62 CS / CS 908 $ 180,000 $ 596,000
E-209 Floating Head 8.62 8.62 CS / CS 62.4 $ 30,400 $ 101,000
E-210 Floating Head 1 1 CS / CS 100 $ 36,100 $ 119,000
E-211 Floating Head 1.72 1.72 CS / CS 9.66 $ 28,300 $ 93,000
69
Pumps
(with
drives) Pump Type
Power
(kilowatts) # Spares MOC
Discharge
Pressure
(barg)
Purchased
Equipment Cost
Bare Module
Cost
P-201 Centrifugal 2.09 1 CS 1.72 $ 7,520 $ 30,000
P-202 Centrifugal 1.34 1 CS 1.72 $ 7,120 $ 28,400
P-203 Centrifugal 2.29 1 CS 1.72 $ 7,630 $ 30,400
P-204 Centrifugal 1.79 1 CS 1.72 $ 7,360 $ 29,300
Reactors Type
Volume
(cubic
meters)
Purchased
Equipment Cost
Bare Module
Cost
R-201
Jacketed Non-
Agitated 1.18 $ 10,200 $ 15,300
Towers
Tower
Description
Height
(meters)
Diameter
(meters) Tower MOC
Demister
MOC
Pressure
(barg)
Purchased
Equipment Cost
Bare Module
Cost
T-201 10 CS Valve Trays 7.01 0.305 CS SS 1.72 $ 31,200 $ 47,400
T-202 20 CS Valve Trays 14.3 0.61 CS SS 25 $ 56,700 $ 119,000
Vessels Orientation
Length/Heig
ht (meters)
Diameter
(meters) MOC
Demister
MOC
Pressure
(barg)
Purchased
Equipment Cost
Bare Module
Cost
V-201 Vertical 8.6 2.87 CS SS 25.5 $ 67,500 $ 947,000
V-202 Horizontal 4.97 1.62 CS 1.72 $ 15,200 $ 45,800
V-203 Horizontal 4.97 1.65 CS 1.72 $ 15,500 $ 46,700
Total Bare Module Cost $ 19,732,300
70
Table A.11. CAPCOST program for the optimization.
Compressors
Compressor
Type
Power
(kilowatts) # Spares MOC
Purchased
Equipment Cost
Bare Module
Cost
C-201 Rotary 202 1 SS $ 532,000 $ 2,680,000
C-202 Rotary 347 1 CS $1,740,000 $ 4,200,000
C-203 Rotary 360 1 CS $1,910,000 $ 4,610,000
Exchangers Exchanger Type
Shell
Pressure
(barg)
Tube
Pressure
(barg) MOC
Area
(square meters)
Purchased
Equipment Cost
Bare Module
Cost
E-201 Floating Head 42.4 42.4 CS / CS 157 $ 44,900 $ 161,000
E-202 Floating Head 42.7 42.7 SS / CS 17.7 $ 26,200 $ 136,000
E-203 Floating Head 25 25 CS / CS 37.9 $ 27,200 $ 94,000
E-204 Floating Head 42.7 42.7 CS / CS 212 $ 53,600 $ 192,000
E-205 Floating Head 1 1 CS / CS 69 $ 31,400 $ 103,000
E-206 Floating Head 2.07 2.07 CS / CS 287 $ 65,700 $ 216,000
E-207 Floating Head 2.07 2.07 CS / CS 136 $ 41,600 $ 137,000
E-208 Floating Head 8.62 8.62 CS / CS 595 $ 119,000 $ 394,000
E-209 Floating Head 8.62 8.62 CS / CS 62.4 $ 30,400 $ 101,000
E-210 Double Pipe 1 CS / CS 9.66 $ 5,270 $ 17,400
E-211 Double Pipe 1.72 CS / CS 5.85 $ 4,790 $ 15,800
E-212 Double Pipe 2.41 CS / CS 0.65 $ 3,140 $ 10,300
E-213 Double Pipe 2.41 CS / CS 0.557 $ 3,140 $ 10,300
71
Pumps
(with
drives) Pump Type
Power
(kilowatts) # Spares MOC
Discharge
Pressure
(barg)
Purchased
Equipment
Cost
Bare Module
Cost
P-201 Centrifugal 2.09 1 CS 1.72 $ 7,520 $ 30,000
P-202 Centrifugal 1.34 1 CS 1.72 $ 7,120 $ 28,400
P-203 Centrifugal 2.29 1 CS 1.72 $ 7,630 $ 30,400
P-204 Centrifugal 1.79 1 CS 1.72 $ 7,360 $ 29,300
P-205 Centrifugal 0.033 1 CS 1.72 $ 6,970 $ 27,800
P-206 Centrifugal 0.023 1 Cast Iron 1.72 $ 6,970 $ 22,600
Reactors Type
Volume
(cubic meters)
Purchased
Equipment
Cost
Bare Module
Cost
R-201 Jacketed Non-Agitated 1.18 $ 10,200 $ 15,300
Towers Tower Description
Height
(meters)
Diameter
(meters)
Tower
MOC
Demister
MOC
Pressure
(barg)
Purchased
Equipment
Cost
Bare Module
Cost
T-201 10 CS Valve Trays 7.01 0.305 CS SS 1.72 $ 31,200 $ 47,400
T-202 20 CS Valve Trays 14.3 0.61 CS SS 25 $ 56,700 $ 119,000
T-203 6 CS Valve Trays 4.27 0.183 CS SS 2.41 $ 29,400 $ 40,500
Vessels Orientation
Length/Height
(meters)
Diameter
(meters) MOC
Demister
MOC
Pressure
(barg)
Purchased
Equipment
Cost
Bare Module
Cost
V-201 Vertical 8.6 2.87 CS SS 25.5 $ 67,500 $ 947,000
V-202 Horizontal 4.97 1.62 CS 1.72 $ 15,200 $ 45,800
V-203 Horizontal 4.97 1.65 CS 1.72 $ 15,500 $ 46,700
V-204 Horizontal 1.22 0.396 CS 2.41 $ 2,890 $ 8,680
Total Bare Module Cost $14,516,680
72
Grassroots Cost:
(80)
(81)
Operator Labor Cost:
( )
(82)
(83)
( ) (84)
(85)
(86)
Raw Material Cost:
(87)
(88)
(89)
Waste Treatment Cost:
(90)
(91)
(92)
Cost of Manufacture:
( ) (93)
(
) (94)
73
Deprecation:
(95)
(96)
Table A.12. MACRS Method
Year Depreciation Allowance (%)
3 20
4 32
5 19.20
6 11.52
7 11.52
8 5.76
Revenue:
(97)
After Tax Profit:
( ) ( ) (98)
( ) ( ) (99)
(100)
After Tax Cash Flow:
(101)
(102)
Discounted Cash Flow:
( ) (103)
( ) (104)
(105)
74
Appendix B – Aspen Input Summaries
Production of Maleic Anhydride from n-Butane
;;Input Summary created by Aspen Plus Rel. 25.0 at 14:41:30 Sun Dec 4, 2011
;Directory C:\Users\ljcfy3\Downloads Filename
C:\Users\ljcfy3\AppData\Local\Temp\~apd74a.txt
;
DYNAMICS
DYNAMICS RESULTS=ON
TITLE 'Production of Maleic Anhydride'
IN-UNITS ENG
DEF-STREAMS CONVEN ALL
SIM-OPTIONS
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
SIM-OPTIONS MASS-BAL-CHE=YES OLD-DATABANK=YES
DESCRIPTION "
General Simulation with Metric Units :
C, bar, kg/hr, kmol/hr, Gcal/hr, cum/hr.
Property Method: None
Flow basis for input: Mass
Stream report composition: Mass flow
"
DATABANKS PURE25 / AQUEOUS / SOLIDS / INORGANIC / &
NOASPENPCD
75
PROP-SOURCES PURE25 / AQUEOUS / SOLIDS / INORGANIC
COMPONENTS
WATER H2O /
BUTANE C4H10-1 /
AIR AIR /
OXYGEN O2 /
MAH C4H2O3 /
CO CO /
CO2 CO2 /
FORMIC CH2O2 /
ACRYLIC C3H4O2-1 /
N2 N2 /
MA C4H4O4-D2 /
THF C4H8O-4 /
BUTANOL C4H10O-1 /
PROPANOL C3H8O-1 /
METHANOL CH4O /
H2 H2 /
GAMMA-01 C4H6O2-D2 /
1:4-B-01 C4H10O2-D2 /
METHANE CH4 /
PROPANE C3H8 /
SUCCI-02 C4H6O4-2
FLOWSHEET
BLOCK R-101 IN=7 OUT=8
BLOCK M-101 IN=6 4 OUT=7
BLOCK E-102 IN=8 OUT=9
BLOCK T-101 IN=9 12 OUT=13 15A
BLOCK H-103 IN=16 OUT=17
BLOCK T-101R IN=15A OUT=15
BLOCK R-102 IN=27 OUT=28
BLOCK E-105 IN=26 OUT=27
BLOCK T-103 IN=28 OUT=33 37
BLOCK E-101 IN=11 OUT=12
BLOCK P-101 IN=10 OUT=11
BLOCK T-102 IN=17 OUT=22 26
BLOCK P-103 IN=15 OUT=16
76
BLOCK C-101 IN=2 OUT=5
BLOCK H-102 IN=5 OUT=6
BLOCK P-102 IN=1 OUT=3
BLOCK H-101 IN=3 OUT=4
PROPERTIES NRTL
PROPERTIES B-PITZER / IDEAL / NRTL-2 / PENG-ROB / PSRK /
RK-SOAVE / SRK / UNIQ-2 / UNIQUAC / WILS-RK /
WILS-VOL / WILSON
PROP-DATA BWRKT-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST BWRKT
BPVAL WATER BUTANE .7402200000
BPVAL WATER CO2 -.0795000000
BPVAL WATER N2 -.3032300000
BPVAL WATER H2 -.3556800000
BPVAL WATER METHANE .7872800000
BPVAL BUTANE CO2 .1957800000
BPVAL BUTANE N2 .0865300000
BPVAL BUTANE WATER .7402200000
BPVAL BUTANE H2 -.1459200000
BPVAL BUTANE METHANE .1075300000
BPVAL CO2 BUTANE .1957800000
BPVAL CO2 N2 -.0892100000
BPVAL CO2 WATER -.0795000000
BPVAL CO2 H2 -.3993500000
BPVAL CO2 METHANE 8.78000000E-3
BPVAL CO2 PROPANE .1514400000
BPVAL N2 BUTANE .0865300000
BPVAL N2 CO2 -.0892100000
BPVAL N2 WATER -.3032300000
BPVAL N2 H2 -.0837800000
BPVAL N2 METHANE .0361900000
BPVAL N2 PROPANE .1122100000
77
BPVAL CO H2 .4534900000
BPVAL CO PROPANE .0555300000
BPVAL H2 BUTANE -.1459200000
BPVAL H2 CO2 -.3993500000
BPVAL H2 N2 -.0837800000
BPVAL H2 WATER -.3556800000
BPVAL H2 CO .4534900000
BPVAL H2 METHANE -.4387400000
BPVAL H2 PROPANE -.2514400000
BPVAL METHANE BUTANE .1075300000
BPVAL METHANE CO2 8.78000000E-3
BPVAL METHANE N2 .0361900000
BPVAL METHANE WATER .7872800000
BPVAL METHANE H2 -.4387400000
BPVAL METHANE PROPANE .0631600000
BPVAL PROPANE CO2 .1514400000
BPVAL PROPANE N2 .1122100000
BPVAL PROPANE H2 -.2514400000
BPVAL PROPANE CO .0555300000
BPVAL PROPANE METHANE .0631600000
PROP-DATA BWRKV-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST BWRKV
BPVAL WATER BUTANE .3183100000
BPVAL WATER CO2 .0605100000
BPVAL WATER N2 .1032000000
BPVAL WATER H2 .1535100000
BPVAL WATER METHANE .2553200000
BPVAL BUTANE CO2 -.0582800000
BPVAL BUTANE N2 -.0766100000
BPVAL BUTANE WATER .3183100000
BPVAL BUTANE H2 -.0770100000
BPVAL BUTANE METHANE -.0300200000
BPVAL CO2 BUTANE -.0582800000
78
BPVAL CO2 N2 -7.1500000E-3
BPVAL CO2 WATER .0605100000
BPVAL CO2 H2 .0156200000
BPVAL CO2 METHANE .0106700000
BPVAL CO2 PROPANE -.0447300000
BPVAL N2 BUTANE -.0766100000
BPVAL N2 CO2 -7.1500000E-3
BPVAL N2 WATER .1032000000
BPVAL N2 H2 -.0211600000
BPVAL N2 METHANE -.0339900000
BPVAL N2 PROPANE -.0341000000
BPVAL CO H2 -.1097400000
BPVAL CO PROPANE -.0453100000
BPVAL H2 BUTANE -.0770100000
BPVAL H2 CO2 .0156200000
BPVAL H2 N2 -.0211600000
BPVAL H2 WATER .1535100000
BPVAL H2 CO -.1097400000
BPVAL H2 METHANE -.1277700000
BPVAL H2 PROPANE -.0689500000
BPVAL METHANE BUTANE -.0300200000
BPVAL METHANE CO2 .0106700000
BPVAL METHANE N2 -.0339900000
BPVAL METHANE WATER .2553200000
BPVAL METHANE H2 -.1277700000
BPVAL METHANE PROPANE -.0118800000
BPVAL PROPANE CO2 -.0447300000
BPVAL PROPANE N2 -.0341000000
BPVAL PROPANE H2 -.0689500000
BPVAL PROPANE CO -.0453100000
BPVAL PROPANE METHANE -.0118800000
PROP-DATA NRTL-1
IN-UNITS ENG
PROP-LIST NRTL
BPVAL WATER ACRYLIC 0.0 1676.270867 .3000000000 0.0 0.0 &
0.0 212.7200023 248.9000020
BPVAL ACRYLIC WATER 0.0 -543.5965757 .3000000000 0.0 0.0 &
0.0 212.7200023 248.9000020
BPVAL WATER THF 4.760148000 -1320.122869 .4725526000 0.0 &
79
0.0 0.0 146.1380028 212.0000023
BPVAL THF WATER 1.214162000 284.0056177 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL WATER BUTANOL 13.11020000 -6010.116432 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL BUTANOL WATER -2.040500000 1374.964549 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL ACRYLIC BUTANOL 0.0 -1073.497311 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL BUTANOL ACRYLIC 0.0 970.5745722 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL THF BUTANOL 0.0 607.2393551 .3000000000 0.0 0.0 0.0 &
154.9400028 224.8700022
BPVAL BUTANOL THF 0.0 -354.7387772 .3000000000 0.0 0.0 &
0.0 154.9400028 224.8700022
BPVAL WATER PROPANOL 5.448600000 -1550.122548 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL PROPANOL WATER -1.741100000 1037.602432 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL BUTANE PROPANOL 0.0 566.5037355 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL PROPANOL BUTANE 0.0 347.8390172 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL ACRYLIC PROPANOL 0.0 2188.951182 .3000000000 0.0 0.0 &
0.0 212.0000023 284.0000017
BPVAL PROPANOL ACRYLIC 0.0 -1335.879709 .3000000000 0.0 &
0.0 0.0 212.0000023 284.0000017
BPVAL THF PROPANOL 0.0 708.9470943 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL PROPANOL THF 0.0 -399.7814368 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL BUTANOL PROPANOL 0.0 -158.9718587 .3000000000 0.0 &
0.0 0.0 104.0000032 243.6800021
BPVAL PROPANOL BUTANOL 0.0 203.3026184 .3000000000 0.0 0.0 &
0.0 104.0000032 243.6800021
BPVAL WATER METHANOL 2.732200000 -1111.083651 .3000000000 &
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL METHANOL WATER -.6930000000 311.3767775 .3000000000 &
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL BUTANE METHANOL 0.0 993.1037321 .3000000000 0.0 0.0 &
80
0.0 122.0000030 122.0000030
BPVAL METHANOL BUTANE 0.0 684.7795745 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL THF METHANOL 0.0 403.4712568 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL METHANOL THF 0.0 113.5891791 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL BUTANOL METHANOL -1.516500000 436.7237365 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL METHANOL BUTANOL 2.220000000 -607.8823151 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL PROPANOL METHANOL 0.0 -15.99605987 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL METHANOL PROPANOL 0.0 35.19845972 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL WATER GAMMA-01 0.0 1474.941048 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL GAMMA-01 WATER 0.0 -88.62929929 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL THF GAMMA-01 16.04880000 -8348.314613 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL GAMMA-01 THF .9873000000 -1378.530169 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL WATER 1:4-B-01 0.0 1381.130629 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL 1:4-B-01 WATER 0.0 992.9431721 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL THF 1:4-B-01 -9.196000000 6646.489327 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 THF 7.301800000 -4588.857323 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL METHANOL 1:4-B-01 .3892000000 109.6928991 .3000000000 &
0.0 0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 METHANOL -.0611000000 -342.0120573 &
.3000000000 0.0 0.0 0.0 140.0000029 439.7000005
PROP-DATA NRTL-2
IN-UNITS ENG
PROP-LIST NRTL 2
BPVAL WATER ACRYLIC 0.0 1676.270867 .3000000000 0.0 0.0 &
81
0.0 212.7200023 248.9000020
BPVAL ACRYLIC WATER 0.0 -543.5965757 .3000000000 0.0 0.0 &
0.0 212.7200023 248.9000020
BPVAL WATER THF 4.760148000 -1320.122869 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL THF WATER 1.214162000 284.0056177 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL WATER BUTANOL 13.11020000 -6010.116432 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL BUTANOL WATER -2.040500000 1374.964549 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL ACRYLIC BUTANOL 0.0 -1073.497311 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL BUTANOL ACRYLIC 0.0 970.5745722 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL THF BUTANOL 0.0 607.2393551 .3000000000 0.0 0.0 0.0 &
154.9400028 224.8700022
BPVAL BUTANOL THF 0.0 -354.7387772 .3000000000 0.0 0.0 &
0.0 154.9400028 224.8700022
BPVAL WATER PROPANOL 5.448600000 -1550.122548 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL PROPANOL WATER -1.741100000 1037.602432 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL BUTANE PROPANOL 0.0 566.5037355 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL PROPANOL BUTANE 0.0 347.8390172 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL ACRYLIC PROPANOL 0.0 2188.951182 .3000000000 0.0 0.0 &
0.0 212.0000023 284.0000017
BPVAL PROPANOL ACRYLIC 0.0 -1335.879709 .3000000000 0.0 &
0.0 0.0 212.0000023 284.0000017
BPVAL THF PROPANOL 0.0 708.9470943 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL PROPANOL THF 0.0 -399.7814368 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL BUTANOL PROPANOL 0.0 -158.9718587 .3000000000 0.0 &
0.0 0.0 104.0000032 243.6800021
BPVAL PROPANOL BUTANOL 0.0 203.3026184 .3000000000 0.0 0.0 &
0.0 104.0000032 243.6800021
BPVAL WATER METHANOL 2.732200000 -1111.083651 .3000000000 &
82
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL METHANOL WATER -.6930000000 311.3767775 .3000000000 &
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL BUTANE METHANOL 0.0 993.1037321 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL METHANOL BUTANE 0.0 684.7795745 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL THF METHANOL 0.0 403.4712568 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL METHANOL THF 0.0 113.5891791 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL BUTANOL METHANOL -1.516500000 436.7237365 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL METHANOL BUTANOL 2.220000000 -607.8823151 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL PROPANOL METHANOL 0.0 -15.99605987 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL METHANOL PROPANOL 0.0 35.19845972 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL WATER GAMMA-01 0.0 1474.941048 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL GAMMA-01 WATER 0.0 -88.62929929 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL THF GAMMA-01 16.04880000 -8348.314613 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL GAMMA-01 THF .9873000000 -1378.530169 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL WATER 1:4-B-01 0.0 1381.130629 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL 1:4-B-01 WATER 0.0 992.9431721 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL THF 1:4-B-01 -9.196000000 6646.489327 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 THF 7.301800000 -4588.857323 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL METHANOL 1:4-B-01 .3892000000 109.6928991 .3000000000 &
0.0 0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 METHANOL -.0611000000 -342.0120573 &
.3000000000 0.0 0.0 0.0 140.0000029 439.7000005
83
PROP-DATA PRKBV-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST PRKBV
BPVAL WATER CO2 .1200000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 WATER .1200000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE CO2 .1333000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 BUTANE .1333000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE N2 .0800000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 BUTANE .0800000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL OXYGEN N2 -.0119000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 OXYGEN -.0119000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO N2 .0307000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO .0307000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 N2 -.0170000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO2 -.0170000000 0.0 0.0 -273.1500000 726.8500000
BPVAL WATER METHANOL -.0778000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL WATER -.0778000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANOL .0230000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL CO2 .0230000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 METHANOL -.2141000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL N2 -.2141000000 0.0 0.0 -273.1500000 &
726.8500000
84
BPVAL BUTANE H2 -.3970000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 BUTANE -.3970000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO H2 .0919000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO .0919000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 H2 -.1622000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO2 -.1622000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 H2 .1030000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 N2 .1030000000 0.0 0.0 -273.1500000 726.8500000
BPVAL BUTANE METHANE .0133000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE BUTANE .0133000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO METHANE .0300000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO .0300000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANE .0919000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO2 .0919000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 METHANE .0311000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE N2 .0311000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 METHANE .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE H2 .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE PROPANE 3.30000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE BUTANE 3.30000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO PROPANE .0259000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE CO .0259000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 PROPANE .1241000000 0.0 0.0 -273.1500000 &
726.8500000
85
BPVAL PROPANE CO2 .1241000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 PROPANE .0852000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE N2 .0852000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 PROPANE -.0833000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE H2 -.0833000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE PROPANE .0140000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE METHANE .0140000000 0.0 0.0 -273.1500000 &
726.8500000
PROP-DATA RKSKBV-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST RKSKBV
BPVAL WATER CO2 .0737000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 WATER .0737000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE CO2 .1430000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 BUTANE .1430000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE N2 .0700000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 BUTANE .0700000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL OXYGEN N2 -7.8000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 OXYGEN -7.8000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO N2 .0374000000 0.0 0.0 -273.1500000 726.8500000
86
BPVAL N2 CO .0374000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 N2 -.0315000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO2 -.0315000000 0.0 0.0 -273.1500000 726.8500000
BPVAL WATER METHANOL -.0789000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL WATER -.0789000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANOL .0148000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL CO2 .0148000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 METHANOL -.2881000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL N2 -.2881000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE H2 -.5100000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 BUTANE -.5100000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO H2 .0804000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO .0804000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 H2 -.3426000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO2 -.3426000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 H2 .0978000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 N2 .0978000000 0.0 0.0 -273.1500000 726.8500000
BPVAL BUTANE METHANE 5.60000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE BUTANE 5.60000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO METHANE .0322000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO .0322000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANE .0933000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO2 .0933000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 METHANE .0278000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE N2 .0278000000 0.0 0.0 -273.1500000 &
87
726.8500000
BPVAL H2 METHANE -.0222000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE H2 -.0222000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE PROPANE 0.0 0.0 0.0 -273.1500000 726.8500000
BPVAL PROPANE BUTANE 0.0 0.0 0.0 -273.1500000 726.8500000
BPVAL CO PROPANE .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE CO .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 PROPANE .1289000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE CO2 .1289000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 PROPANE .0763000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE N2 .0763000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 PROPANE -.2359000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE H2 -.2359000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE PROPANE 9.00000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE METHANE 9.00000000E-3 0.0 0.0 -273.1500000 &
726.8500000
PROP-DATA SRKKIJ-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST SRKKIJ
BPVAL CO CO2 -.0154400000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 CO -.0154400000 0.0 0.0 -273.1500000 726.8500000
BPVAL BUTANE METHANE .0226440000 0.0 0.0 -273.1500000 &
726.8500000
88
BPVAL METHANE BUTANE .0226440000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 METHANE -.0244851000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE H2 -.0244851000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE PROPANE -2.0759400E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE BUTANE -2.0759400E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 PROPANE .1014650000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE H2 .1014650000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE PROPANE .0241509000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE METHANE .0241509000 0.0 0.0 -273.1500000 &
726.8500000
PROP-DATA UNIQ-1
IN-UNITS ENG
PROP-LIST UNIQ
BPVAL WATER FORMIC 0.0 420.2459966 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL FORMIC WATER 0.0 278.9279978 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL WATER ACRYLIC 0.0 -815.2817335 0.0 0.0 212.7200023 &
248.9000020 0.0
BPVAL ACRYLIC WATER 0.0 455.6541564 0.0 0.0 212.7200023 &
248.9000020 0.0
BPVAL WATER THF -.3878309000 425.0131166 0.0 0.0 &
146.1380028 212.0000023 0.0
BPVAL THF WATER .3109718000 -1099.904031 0.0 0.0 &
146.1380028 212.0000023 0.0
BPVAL WATER BUTANOL -4.993400000 2824.291597 0.0 0.0 &
66.50600347 243.6800021 0.0
BPVAL BUTANOL WATER 3.764400000 -2603.900319 0.0 0.0 &
66.50600347 243.6800021 0.0
BPVAL ACRYLIC BUTANOL 0.0 572.3542754 0.0 0.0 248.0000020 &
284.0000017 0.0
89
BPVAL BUTANOL ACRYLIC 0.0 -616.4940551 0.0 0.0 248.0000020 &
284.0000017 0.0
BPVAL THF BUTANOL 0.0 -406.3535967 0.0 0.0 154.9400028 &
224.8700022 0.0
BPVAL BUTANOL THF 0.0 270.7903778 0.0 0.0 154.9400028 &
224.8700022 0.0
BPVAL WATER PROPANOL -2.333000000 1080.883071 0.0 0.0 &
77.00000338 212.0000023 0.0
BPVAL PROPANOL WATER 1.766800000 -1172.243151 0.0 0.0 &
77.00000338 212.0000023 0.0
BPVAL BUTANE PROPANOL 0.0 -273.6566978 0.0 0.0 50.00000360 &
104.0000032 0.0
BPVAL PROPANOL BUTANE 0.0 -60.55145952 0.0 0.0 50.00000360 &
104.0000032 0.0
BPVAL ACRYLIC PROPANOL 0.0 -1859.684385 0.0 0.0 &
212.0000023 284.0000017 0.0
BPVAL PROPANOL ACRYLIC 0.0 834.8853533 0.0 0.0 212.0000023 &
284.0000017 0.0
BPVAL THF PROPANOL 0.0 -483.8293761 0.0 0.0 150.4400028 &
207.3200023 0.0
BPVAL PROPANOL THF 0.0 310.2845375 0.0 0.0 150.4400028 &
207.3200023 0.0
BPVAL BUTANOL PROPANOL 0.0 53.83709957 0.0 0.0 104.0000032 &
243.6800021 0.0
BPVAL PROPANOL BUTANOL 0.0 -71.30987943 0.0 0.0 &
104.0000032 243.6800021 0.0
BPVAL WATER METHANOL .6437000000 -579.8361554 0.0 0.0 &
76.98200338 212.0000023 0.0
BPVAL METHANOL WATER -1.066200000 779.1812938 0.0 0.0 &
76.98200338 212.0000023 0.0
BPVAL BUTANE METHANOL 0.0 -1148.501691 0.0 0.0 122.0000030 &
122.0000030 0.0
BPVAL METHANOL BUTANE 0.0 -23.68817981 0.0 0.0 122.0000030 &
122.0000030 0.0
BPVAL THF METHANOL 0.0 -572.5058354 0.0 0.0 87.53000330 &
144.6800028 0.0
BPVAL METHANOL THF 0.0 161.6754587 0.0 0.0 87.53000330 &
144.6800028 0.0
BPVAL BUTANOL METHANOL .2267000000 -225.5174982 0.0 0.0 &
77.00000338 243.8960020 0.0
90
BPVAL METHANOL BUTANOL -.3136000000 148.7455188 0.0 0.0 &
77.00000338 243.8960020 0.0
BPVAL PROPANOL METHANOL 0.0 -167.8472987 0.0 0.0 &
140.0360029 206.8160023 0.0
BPVAL METHANOL PROPANOL 0.0 88.58789929 0.0 0.0 &
140.0360029 206.8160023 0.0
BPVAL WATER GAMMA-01 0.0 31.23053975 0.0 0.0 152.7800028 &
327.1640014 0.0
BPVAL GAMMA-01 WATER 0.0 -225.8560782 0.0 0.0 152.7800028 &
327.1640014 0.0
BPVAL THF GAMMA-01 -11.99890000 6474.853568 0.0 0.0 &
152.7440028 352.6160012 0.0
BPVAL GAMMA-01 THF 1.109300000 -207.5934583 0.0 0.0 &
152.7440028 352.6160012 0.0
BPVAL WATER 1:4-B-01 0.0 249.0355780 0.0 0.0 212.1800023 &
222.8000022 0.0
BPVAL 1:4-B-01 WATER 0.0 -1235.539610 0.0 0.0 212.1800023 &
222.8000022 0.0
BPVAL THF 1:4-B-01 2.601800000 -1934.671305 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL 1:4-B-01 THF -2.501400000 1594.517927 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL METHANOL 1:4-B-01 -.1912000000 383.7301169 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL 1:4-B-01 METHANOL .3393000000 -660.7933147 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL WATER SUCCI-02 0.0 152.7533988 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL SUCCI-02 WATER 0.0 -15.60689988 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL BUTANOL SUCCI-02 0.0 -251.2979980 0.0 0.0 &
68.00000346 104.0000032 0.0
BPVAL SUCCI-02 BUTANOL 0.0 181.7819985 0.0 0.0 68.00000346 &
104.0000032 0.0
PROP-DATA UNIQ-2
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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' &
91
MASS-ENTHALP='kcal/kg' HEAT=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST UNIQ 2
BPVAL WATER FORMIC 0.0 233.4700000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL FORMIC WATER 0.0 154.9600000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL WATER ACRYLIC 0.0 -452.9343000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL ACRYLIC WATER 0.0 253.1412000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL WATER THF -.3878309000 236.1184000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL THF WATER .3109718000 -611.0578000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL WATER BUTANOL -4.993400000 1569.050900 0.0 0.0 &
19.17000000 117.6000000 0.0
BPVAL BUTANOL WATER 3.764400000 -1446.611300 0.0 0.0 &
19.17000000 117.6000000 0.0
BPVAL ACRYLIC BUTANOL 0.0 317.9746000 0.0 0.0 120.0000000 &
140.0000000 0.0
BPVAL BUTANOL ACRYLIC 0.0 -342.4967000 0.0 0.0 120.0000000 &
140.0000000 0.0
BPVAL THF BUTANOL 0.0 -225.7520000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL BUTANOL THF 0.0 150.4391000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL WATER PROPANOL -2.333000000 600.4906000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL PROPANOL WATER 1.766800000 -651.2462000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL BUTANE PROPANOL 0.0 -152.0315000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL PROPANOL BUTANE 0.0 -33.63970000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL ACRYLIC PROPANOL 0.0 -1033.158000 0.0 0.0 &
100.0000000 140.0000000 0.0
BPVAL PROPANOL ACRYLIC 0.0 463.8252000 0.0 0.0 100.0000000 &
140.0000000 0.0
BPVAL THF PROPANOL 0.0 -268.7941000 0.0 0.0 65.80000000 &
92
97.40000000 0.0
BPVAL PROPANOL THF 0.0 172.3803000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL BUTANOL PROPANOL 0.0 29.90950000 0.0 0.0 40.00000000 &
117.6000000 0.0
BPVAL PROPANOL BUTANOL 0.0 -39.61660000 0.0 0.0 &
40.00000000 117.6000000 0.0
BPVAL WATER METHANOL .6437000000 -322.1312000 0.0 0.0 &
24.99000000 100.0000000 0.0
BPVAL METHANOL WATER -1.066200000 432.8785000 0.0 0.0 &
24.99000000 100.0000000 0.0
BPVAL BUTANE METHANOL 0.0 -638.0565000 0.0 0.0 50.00000000 &
50.00000000 0.0
BPVAL METHANOL BUTANE 0.0 -13.16010000 0.0 0.0 50.00000000 &
50.00000000 0.0
BPVAL THF METHANOL 0.0 -318.0588000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL METHANOL THF 0.0 89.81970000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL BUTANOL METHANOL .2267000000 -125.2875000 0.0 0.0 &
25.00000000 117.7200000 0.0
BPVAL METHANOL BUTANOL -.3136000000 82.63640000 0.0 0.0 &
25.00000000 117.7200000 0.0
BPVAL PROPANOL METHANOL 0.0 -93.24850000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL METHANOL PROPANOL 0.0 49.21550000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL WATER GAMMA-01 0.0 17.35030000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL GAMMA-01 WATER 0.0 -125.4756000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL THF GAMMA-01 -11.99890000 3597.140900 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL GAMMA-01 THF 1.109300000 -115.3297000 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL WATER 1:4-B-01 0.0 138.3531000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL 1:4-B-01 WATER 0.0 -686.4109000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL THF 1:4-B-01 2.601800000 -1074.817400 0.0 0.0 &
93
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 THF -2.501400000 885.8433000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL METHANOL 1:4-B-01 -.1912000000 213.1834000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 METHANOL .3393000000 -367.1074000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL WATER SUCCI-02 0.0 84.86300000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL SUCCI-02 WATER 0.0 -8.670500000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL BUTANOL SUCCI-02 0.0 -139.6100000 0.0 0.0 &
20.00000000 40.00000000 0.0
BPVAL SUCCI-02 BUTANOL 0.0 100.9900000 0.0 0.0 20.00000000 &
40.00000000 0.0
PROP-DATA WILSON-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST WILSON
BPVAL WATER ACRYLIC 0.0 168.4465000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL ACRYLIC WATER 0.0 -882.7916000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL WATER THF 1.166967000 -861.2151000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL THF WATER -9.570150000 2146.342000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL WATER BUTANOL .6102000000 -420.6027000 0.0 0.0 &
19.17000000 191.8000000 0.0
BPVAL BUTANOL WATER 2.450400000 -2492.023400 0.0 0.0 &
19.17000000 191.8000000 0.0
BPVAL THF BUTANOL 0.0 180.6092000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL BUTANOL THF 0.0 -388.8284000 0.0 0.0 68.30000000 &
107.1500000 0.0
94
BPVAL WATER PROPANOL 1.267500000 -580.1956000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL PROPANOL WATER -4.815800000 648.7817000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL BUTANE PROPANOL 0.0 -236.3575000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL PROPANOL BUTANE 0.0 -393.1257000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL THF PROPANOL 0.0 133.2163000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL PROPANOL THF 0.0 -299.9573000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL BUTANOL PROPANOL 0.0 -107.5577000 0.0 0.0 &
40.00000000 117.6000000 0.0
BPVAL PROPANOL BUTANOL 0.0 78.37730000 0.0 0.0 40.00000000 &
117.6000000 0.0
BPVAL WATER METHANOL -1.884200000 617.4097000 0.0 0.0 &
24.99000000 188.3000000 0.0
BPVAL METHANOL WATER 1.083700000 -580.2370000 0.0 0.0 &
24.99000000 188.3000000 0.0
BPVAL BUTANE METHANOL -.4811000000 -433.3017000 0.0 0.0 &
50.00000000 100.0000000 0.0
BPVAL METHANOL BUTANE 3.617800000 -1967.833100 0.0 0.0 &
50.00000000 100.0000000 0.0
BPVAL THF METHANOL 0.0 -95.32840000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL METHANOL THF 0.0 -201.7985000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL BUTANOL METHANOL -.6341000000 -73.65750000 0.0 0.0 &
25.00000000 285.4000000 0.0
BPVAL METHANOL BUTANOL .5587000000 -19.02890000 0.0 0.0 &
25.00000000 285.4000000 0.0
BPVAL PROPANOL METHANOL 0.0 -66.18770000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL METHANOL PROPANOL 0.0 47.93730000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL WATER GAMMA-01 0.0 -44.70750000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL GAMMA-01 WATER 0.0 -993.0518000 0.0 0.0 67.10000000 &
163.9800000 0.0
95
BPVAL THF GAMMA-01 -.2082000000 308.0572000 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL GAMMA-01 THF -30.94190000 10000.00000 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL WATER 1:4-B-01 0.0 -506.5348000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL 1:4-B-01 WATER 0.0 -841.3055000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL THF 1:4-B-01 -7.241300000 2413.589800 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 THF 8.514000000 -3389.141600 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL METHANOL 1:4-B-01 -.1189000000 201.7588000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 METHANOL -.5852000000 42.67770000 0.0 0.0 &
60.00000000 226.5000000 0.0
STREAM 1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
SUBSTREAM MIXED TEMP=70. <F> PRES=16. <psig> &
MASS-FLOW=5500.45 <lb/hr> FREE-WATER=NO NPHASE=1 PHASE=L
MASS-FRAC BUTANE 1.
STREAM 2
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
SUBSTREAM MIXED TEMP=68. <F> PRES=101.896 <kPa> &
MASS-FLOW=84736.3 <lb/hr> FREE-WATER=NO NPHASE=1 PHASE=V
MASS-FRAC WATER 0.005844 / OXYGEN 0.233128 / CO2 &
0.000594 / N2 0.760434
96
STREAM 10
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
SUBSTREAM MIXED TEMP=14.889 PRES=101.896 <kPa> &
MASS-FLOW=30887.2 <lb/hr>
MASS-FRAC WATER 1.
BLOCK M-101 MIXER
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROPERTIES NRTL FREE-WATER=STEAM-TA SOLU-WATER=3 &
TRUE-COMPS=YES
BLOCK E-101 HEATER
PARAM TEMP=95. <C> PRES=170. <kPa> NPHASE=1 PHASE=L
BLOCK-OPTION FREE-WATER=NO
BLOCK E-102 HEATER
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM TEMP=95. PRES=170. <kPa>
BLOCK E-105 HEATER
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
97
PDROP=bar
PARAM TEMP=40. PRES=200. <kPa>
BLOCK H-101 HEATER
PARAM TEMP=410. <C> PRES=275. <kPa>
BLOCK H-102 HEATER
PARAM TEMP=410. <C> PRES=275. <kPa>
BLOCK H-103 HEATER
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM TEMP=300. PRES=200. <kPa> NPHASE=1 PHASE=L
BLOCK T-101 RADFRAC
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM NSTAGE=3
COL-CONFIG CONDENSER=NONE REBOILER=NONE
RATESEP-ENAB CALC-MODE=EQUILIBRIUM
FEEDS 9 3 ON-STAGE-VAP / 12 1
PRODUCTS 13 1 V / 15A 3 L
P-SPEC 1 170. <kPa> / 2 170. <kPa>
COL-SPECS
PROPERTIES NRTL FREE-WATER=STEAM-TA SOLU-WATER=3 &
TRUE-COMPS=YES
BLOCK T-102 RADFRAC
PARAM NSTAGE=30
COL-CONFIG CONDENSER=TOTAL
FEEDS 17 3
PRODUCTS 22 1 L / 26 30 L
98
P-SPEC 1 200. <kPa> / 2 200. <kPa>
COL-SPECS D:F=0.946 MOLE-RR=0.06
PROPERTIES NRTL FREE-WATER=STEAM-TA SOLU-WATER=3 &
TRUE-COMPS=YES
REPORT STDVPROF
BLOCK T-103 RADFRAC
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM NSTAGE=30
COL-CONFIG CONDENSER=TOTAL
FEEDS 28 17
PRODUCTS 33 1 L / 37 30 L
P-SPEC 1 200. <kPa> / 2 200. <kPa>
COL-SPECS D:F=0.51559001 MOLE-RR=0.10363926
PROPERTIES NRTL FREE-WATER=STEAM-TA SOLU-WATER=3 &
TRUE-COMPS=YES
REPORT STDVPROF
BLOCK R-101 RSTOIC
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM TEMP=410. PRES=275. <kPa> SERIES=YES
STOIC 1 MIXED BUTANE -1. / OXYGEN -3.5 / MAH 1. / &
WATER 4.
STOIC 2 MIXED BUTANE -1. / OXYGEN -5.5 / CO 2. / CO2 &
2. / WATER 5.
STOIC 3 MIXED BUTANE -1. / OXYGEN -3.5 / ACRYLIC 1. / &
CO2 1. / WATER 3.
STOIC 4 MIXED BUTANE -1. / OXYGEN -6. / CO2 3. / &
WATER 4. / FORMIC 1.
CONV 1 MIXED BUTANE 0.822
99
CONV 2 MIXED BUTANE 0.822
CONV 3 MIXED BUTANE 0.822
CONV 4 MIXED BUTANE 0.822
SELECTIVITY 1 MAH MIXED BUTANE MIXED
SELECTIVITY 2 CO MIXED BUTANE MIXED
SELECTIVITY 3 ACRYLIC MIXED BUTANE MIXED
SELECTIVITY 4 FORMIC MIXED BUTANE MIXED
PROPERTIES NRTL FREE-WATER=STEAM-TA SOLU-WATER=3 &
TRUE-COMPS=YES
BLOCK R-102 RSTOIC
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM TEMP=40. PRES=200. <kPa> NPHASE=1 PHASE=L
STOIC 1 MIXED MA -1. / MAH 1. / WATER 1.
CONV 1 MIXED MA 1.
PROPERTIES NRTL FREE-WATER=STEAM-TA SOLU-WATER=3 &
TRUE-COMPS=YES
BLOCK-OPTION FREE-WATER=NO
BLOCK T-101R RSTOIC
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PARAM TEMP=95. PRES=170. <kPa> NPHASE=1 PHASE=L
STOIC 1 MIXED WATER -1. / MAH -1. / MA 1.
CONV 1 MIXED MAH 1.
BLOCK-OPTION FREE-WATER=NO
BLOCK P-101 PUMP
PARAM PRES=170. <kPa> EFF=0.85
BLOCK P-102 PUMP
100
PARAM PRES=275. <kPa> EFF=0.85
BLOCK P-103 PUMP
PARAM PRES=200. <kPa> EFF=0.85
BLOCK C-101 COMPR
PARAM TYPE=ASME-POLYTROP PRES=275. <kPa> MEFF=0.85
EO-CONV-OPTI
CONV-OPTIONS
WEGSTEIN MAXIT=30
STREAM-REPOR MOLEFLOW MASSFLOW MASSFRAC
101
Production of Tetrahydrofuran from Maleic Anhydride
;Input Summary created by Aspen Plus Rel. 25.0 at 14:44:40 Sun Dec 4, 2011
;Directory C:\Users\ljcfy3\Downloads Filename
C:\Users\ljcfy3\AppData\Local\Temp\~apc002.txt
;
DYNAMICS
DYNAMICS RESULTS=ON
TITLE 'Production of Maleic Anhydride'
IN-UNITS ENG
DEF-STREAMS CONVEN ALL
SIM-OPTIONS
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
SIM-OPTIONS MASS-BAL-CHE=YES OLD-DATABANK=YES
DESCRIPTION "
General Simulation with Metric Units :
C, bar, kg/hr, kmol/hr, Gcal/hr, cum/hr.
Property Method: None
Flow basis for input: Mass
Stream report composition: Mass flow
"
DATABANKS PURE25 / AQUEOUS / SOLIDS / INORGANIC / &
NOASPENPCD
PROP-SOURCES PURE25 / AQUEOUS / SOLIDS / INORGANIC
102
COMPONENTS
WATER H2O /
BUTANE C4H10-1 /
AIR AIR /
OXYGEN O2 /
MAH C4H2O3 /
CO CO /
CO2 CO2 /
FORMIC CH2O2 /
ACRYLIC C3H4O2-1 /
N2 N2 /
MA C4H4O4-D2 /
THF C4H8O-4 /
BUTANOL C4H10O-1 /
PROPANOL C3H8O-1 /
METHANOL CH4O /
H2 H2 /
GAMMA-01 C4H6O2-D2 /
1:4-B-01 C4H10O2-D2 /
METHANE CH4 /
PROPANE C3H8 /
SUCCI-02 C4H6O4-2
FLOWSHEET
BLOCK M-201 IN=38 41 OUT=42
BLOCK R-201 IN=42 49 OUT=43
BLOCK E-203 IN=43 OUT=44
BLOCK E-205 IN=51 OUT=52
BLOCK T-201 IN=52 78 OUT=56 60
BLOCK S-202 IN=66 OUT=74 73
BLOCK V-201 IN=44 OUT=45 50
BLOCK S-201 IN=45 OUT=46 47
BLOCK E-204 IN=48 OUT=49
BLOCK V-204 IN=76 OUT=77 78
BLOCK T-202 IN=62 OUT=66 70
BLOCK CV-203 IN=70 OUT=71
BLOCK E-211 IN=71 OUT=72
BLOCK C-201 IN=47 OUT=48
BLOCK C-202 IN=56 OUT=61
103
BLOCK C-203 IN=61 OUT=62
BLOCK E-210 IN=75 OUT=76
BLOCK T-103P IN=36 OUT=37
BLOCK E-202 IN=37 OUT=38
BLOCK E-201 IN=40 OUT=41
BLOCK CV-201 IN=39 OUT=40
BLOCK CV-202 IN=50 OUT=51
BLOCK CV-204 IN=74 OUT=75
PROPERTIES NRTL
PROPERTIES B-PITZER / IDEAL / NRTL-2 / PENG-ROB / PSRK /
RK-SOAVE / SRK / UNIQ-2 / UNIQUAC / WILS-RK /
WILS-VOL / WILSON
PROP-DATA BWRKT-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST BWRKT
BPVAL WATER BUTANE .7402200000
BPVAL WATER CO2 -.0795000000
BPVAL WATER N2 -.3032300000
BPVAL WATER H2 -.3556800000
BPVAL WATER METHANE .7872800000
BPVAL BUTANE CO2 .1957800000
BPVAL BUTANE N2 .0865300000
BPVAL BUTANE H2 -.1459200000
BPVAL BUTANE METHANE .1075300000
BPVAL BUTANE WATER .7402200000
BPVAL CO2 BUTANE .1957800000
BPVAL CO2 N2 -.0892100000
BPVAL CO2 H2 -.3993500000
BPVAL CO2 METHANE 8.78000000E-3
BPVAL CO2 WATER -.0795000000
BPVAL CO2 PROPANE .1514400000
BPVAL N2 BUTANE .0865300000
BPVAL N2 CO2 -.0892100000
104
BPVAL N2 H2 -.0837800000
BPVAL N2 METHANE .0361900000
BPVAL N2 WATER -.3032300000
BPVAL N2 PROPANE .1122100000
BPVAL CO H2 .4534900000
BPVAL CO PROPANE .0555300000
BPVAL H2 BUTANE -.1459200000
BPVAL H2 CO2 -.3993500000
BPVAL H2 N2 -.0837800000
BPVAL H2 METHANE -.4387400000
BPVAL H2 WATER -.3556800000
BPVAL H2 PROPANE -.2514400000
BPVAL H2 CO .4534900000
BPVAL METHANE BUTANE .1075300000
BPVAL METHANE CO2 8.78000000E-3
BPVAL METHANE N2 .0361900000
BPVAL METHANE H2 -.4387400000
BPVAL METHANE WATER .7872800000
BPVAL METHANE PROPANE .0631600000
BPVAL PROPANE CO2 .1514400000
BPVAL PROPANE N2 .1122100000
BPVAL PROPANE H2 -.2514400000
BPVAL PROPANE METHANE .0631600000
BPVAL PROPANE CO .0555300000
PROP-DATA BWRKV-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST BWRKV
BPVAL WATER BUTANE .3183100000
BPVAL WATER CO2 .0605100000
BPVAL WATER N2 .1032000000
BPVAL WATER H2 .1535100000
BPVAL WATER METHANE .2553200000
BPVAL BUTANE CO2 -.0582800000
BPVAL BUTANE N2 -.0766100000
105
BPVAL BUTANE H2 -.0770100000
BPVAL BUTANE METHANE -.0300200000
BPVAL BUTANE WATER .3183100000
BPVAL CO2 BUTANE -.0582800000
BPVAL CO2 N2 -7.1500000E-3
BPVAL CO2 H2 .0156200000
BPVAL CO2 METHANE .0106700000
BPVAL CO2 WATER .0605100000
BPVAL CO2 PROPANE -.0447300000
BPVAL N2 BUTANE -.0766100000
BPVAL N2 CO2 -7.1500000E-3
BPVAL N2 H2 -.0211600000
BPVAL N2 METHANE -.0339900000
BPVAL N2 WATER .1032000000
BPVAL N2 PROPANE -.0341000000
BPVAL CO H2 -.1097400000
BPVAL CO PROPANE -.0453100000
BPVAL H2 BUTANE -.0770100000
BPVAL H2 CO2 .0156200000
BPVAL H2 N2 -.0211600000
BPVAL H2 METHANE -.1277700000
BPVAL H2 WATER .1535100000
BPVAL H2 PROPANE -.0689500000
BPVAL H2 CO -.1097400000
BPVAL METHANE BUTANE -.0300200000
BPVAL METHANE CO2 .0106700000
BPVAL METHANE N2 -.0339900000
BPVAL METHANE H2 -.1277700000
BPVAL METHANE WATER .2553200000
BPVAL METHANE PROPANE -.0118800000
BPVAL PROPANE CO2 -.0447300000
BPVAL PROPANE N2 -.0341000000
BPVAL PROPANE H2 -.0689500000
BPVAL PROPANE METHANE -.0118800000
BPVAL PROPANE CO -.0453100000
PROP-DATA NRTL-1
IN-UNITS ENG
PROP-LIST NRTL
BPVAL WATER ACRYLIC 0.0 1676.270867 .3000000000 0.0 0.0 &
106
0.0 212.7200023 248.9000020
BPVAL ACRYLIC WATER 0.0 -543.5965757 .3000000000 0.0 0.0 &
0.0 212.7200023 248.9000020
BPVAL WATER THF 4.760148000 -1320.122869 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL THF WATER 1.214162000 284.0056177 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL WATER BUTANOL 13.11020000 -6010.116432 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL BUTANOL WATER -2.040500000 1374.964549 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL ACRYLIC BUTANOL 0.0 -1073.497311 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL BUTANOL ACRYLIC 0.0 970.5745722 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL THF BUTANOL 0.0 607.2393551 .3000000000 0.0 0.0 0.0 &
154.9400028 224.8700022
BPVAL BUTANOL THF 0.0 -354.7387772 .3000000000 0.0 0.0 &
0.0 154.9400028 224.8700022
BPVAL WATER PROPANOL 5.448600000 -1550.122548 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL PROPANOL WATER -1.741100000 1037.602432 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL BUTANE PROPANOL 0.0 566.5037355 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL PROPANOL BUTANE 0.0 347.8390172 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL ACRYLIC PROPANOL 0.0 2188.951182 .3000000000 0.0 0.0 &
0.0 212.0000023 284.0000017
BPVAL PROPANOL ACRYLIC 0.0 -1335.879709 .3000000000 0.0 &
0.0 0.0 212.0000023 284.0000017
BPVAL THF PROPANOL 0.0 708.9470943 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL PROPANOL THF 0.0 -399.7814368 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL BUTANOL PROPANOL 0.0 -158.9718587 .3000000000 0.0 &
0.0 0.0 104.0000032 243.6800021
BPVAL PROPANOL BUTANOL 0.0 203.3026184 .3000000000 0.0 0.0 &
0.0 104.0000032 243.6800021
BPVAL WATER METHANOL 2.732200000 -1111.083651 .3000000000 &
107
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL METHANOL WATER -.6930000000 311.3767775 .3000000000 &
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL BUTANE METHANOL 0.0 993.1037321 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL METHANOL BUTANE 0.0 684.7795745 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL THF METHANOL 0.0 403.4712568 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL METHANOL THF 0.0 113.5891791 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL BUTANOL METHANOL -1.516500000 436.7237365 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL METHANOL BUTANOL 2.220000000 -607.8823151 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL PROPANOL METHANOL 0.0 -15.99605987 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL METHANOL PROPANOL 0.0 35.19845972 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL WATER GAMMA-01 0.0 1474.941048 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL GAMMA-01 WATER 0.0 -88.62929929 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL THF GAMMA-01 16.04880000 -8348.314613 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL GAMMA-01 THF .9873000000 -1378.530169 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL WATER 1:4-B-01 0.0 1381.130629 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL 1:4-B-01 WATER 0.0 992.9431721 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL THF 1:4-B-01 -9.196000000 6646.489327 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 THF 7.301800000 -4588.857323 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL METHANOL 1:4-B-01 .3892000000 109.6928991 .3000000000 &
0.0 0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 METHANOL -.0611000000 -342.0120573 &
.3000000000 0.0 0.0 0.0 140.0000029 439.7000005
108
PROP-DATA NRTL-2
IN-UNITS ENG
PROP-LIST NRTL 2
BPVAL WATER ACRYLIC 0.0 1676.270867 .3000000000 0.0 0.0 &
0.0 212.7200023 248.9000020
BPVAL ACRYLIC WATER 0.0 -543.5965757 .3000000000 0.0 0.0 &
0.0 212.7200023 248.9000020
BPVAL WATER THF 4.760148000 -1320.122869 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL THF WATER 1.214162000 284.0056177 .4725526000 0.0 &
0.0 0.0 146.1380028 212.0000023
BPVAL WATER BUTANOL 13.11020000 -6010.116432 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL BUTANOL WATER -2.040500000 1374.964549 .3000000000 &
0.0 0.0 0.0 66.50600347 243.6800021
BPVAL ACRYLIC BUTANOL 0.0 -1073.497311 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL BUTANOL ACRYLIC 0.0 970.5745722 .3116000000 0.0 0.0 &
0.0 248.0000020 284.0000017
BPVAL THF BUTANOL 0.0 607.2393551 .3000000000 0.0 0.0 0.0 &
154.9400028 224.8700022
BPVAL BUTANOL THF 0.0 -354.7387772 .3000000000 0.0 0.0 &
0.0 154.9400028 224.8700022
BPVAL WATER PROPANOL 5.448600000 -1550.122548 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL PROPANOL WATER -1.741100000 1037.602432 .3000000000 &
0.0 0.0 0.0 77.00000338 212.0000023
BPVAL BUTANE PROPANOL 0.0 566.5037355 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL PROPANOL BUTANE 0.0 347.8390172 .3000000000 0.0 0.0 &
0.0 50.00000360 104.0000032
BPVAL ACRYLIC PROPANOL 0.0 2188.951182 .3000000000 0.0 0.0 &
0.0 212.0000023 284.0000017
BPVAL PROPANOL ACRYLIC 0.0 -1335.879709 .3000000000 0.0 &
0.0 0.0 212.0000023 284.0000017
BPVAL THF PROPANOL 0.0 708.9470943 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL PROPANOL THF 0.0 -399.7814368 .3000000000 0.0 0.0 &
0.0 150.4400028 207.3200023
BPVAL BUTANOL PROPANOL 0.0 -158.9718587 .3000000000 0.0 &
109
0.0 0.0 104.0000032 243.6800021
BPVAL PROPANOL BUTANOL 0.0 203.3026184 .3000000000 0.0 0.0 &
0.0 104.0000032 243.6800021
BPVAL WATER METHANOL 2.732200000 -1111.083651 .3000000000 &
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL METHANOL WATER -.6930000000 311.3767775 .3000000000 &
0.0 0.0 0.0 76.98200338 212.0000023
BPVAL BUTANE METHANOL 0.0 993.1037321 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL METHANOL BUTANE 0.0 684.7795745 .3000000000 0.0 0.0 &
0.0 122.0000030 122.0000030
BPVAL THF METHANOL 0.0 403.4712568 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL METHANOL THF 0.0 113.5891791 .3000000000 0.0 0.0 &
0.0 87.53000330 144.6800028
BPVAL BUTANOL METHANOL -1.516500000 436.7237365 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL METHANOL BUTANOL 2.220000000 -607.8823151 .3000000000 &
0.0 0.0 0.0 77.00000338 243.8960020
BPVAL PROPANOL METHANOL 0.0 -15.99605987 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL METHANOL PROPANOL 0.0 35.19845972 .3000000000 0.0 &
0.0 0.0 140.0360029 206.8160023
BPVAL WATER GAMMA-01 0.0 1474.941048 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL GAMMA-01 WATER 0.0 -88.62929929 .3000000000 0.0 0.0 &
0.0 152.7800028 327.1640014
BPVAL THF GAMMA-01 16.04880000 -8348.314613 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL GAMMA-01 THF .9873000000 -1378.530169 .3000000000 0.0 &
0.0 0.0 152.7440028 352.6160012
BPVAL WATER 1:4-B-01 0.0 1381.130629 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL 1:4-B-01 WATER 0.0 992.9431721 .4700000000 0.0 0.0 &
0.0 212.1800023 222.8000022
BPVAL THF 1:4-B-01 -9.196000000 6646.489327 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 THF 7.301800000 -4588.857323 .3000000000 0.0 &
0.0 0.0 140.0000029 439.7000005
BPVAL METHANOL 1:4-B-01 .3892000000 109.6928991 .3000000000 &
110
0.0 0.0 0.0 140.0000029 439.7000005
BPVAL 1:4-B-01 METHANOL -.0611000000 -342.0120573 &
.3000000000 0.0 0.0 0.0 140.0000029 439.7000005
PROP-DATA PRKBV-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST PRKBV
BPVAL WATER CO2 .1200000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 WATER .1200000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE CO2 .1333000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 BUTANE .1333000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE N2 .0800000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 BUTANE .0800000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL OXYGEN N2 -.0119000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 OXYGEN -.0119000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO N2 .0307000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO .0307000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 N2 -.0170000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO2 -.0170000000 0.0 0.0 -273.1500000 726.8500000
BPVAL WATER METHANOL -.0778000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL WATER -.0778000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANOL .0230000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL CO2 .0230000000 0.0 0.0 -273.1500000 &
726.8500000
111
BPVAL N2 METHANOL -.2141000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL N2 -.2141000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE H2 -.3970000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 BUTANE -.3970000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO H2 .0919000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO .0919000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 H2 -.1622000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO2 -.1622000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 H2 .1030000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 N2 .1030000000 0.0 0.0 -273.1500000 726.8500000
BPVAL BUTANE METHANE .0133000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE BUTANE .0133000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO METHANE .0300000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO .0300000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANE .0919000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO2 .0919000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 METHANE .0311000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE N2 .0311000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 METHANE .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE H2 .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE PROPANE 3.30000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE BUTANE 3.30000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO PROPANE .0259000000 0.0 0.0 -273.1500000 &
726.8500000
112
BPVAL PROPANE CO .0259000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 PROPANE .1241000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE CO2 .1241000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 PROPANE .0852000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE N2 .0852000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 PROPANE -.0833000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE H2 -.0833000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE PROPANE .0140000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE METHANE .0140000000 0.0 0.0 -273.1500000 &
726.8500000
PROP-DATA RKSKBV-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST RKSKBV
BPVAL WATER CO2 .0737000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 WATER .0737000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE CO2 .1430000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 BUTANE .1430000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE N2 .0700000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 BUTANE .0700000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL OXYGEN N2 -7.8000000E-3 0.0 0.0 -273.1500000 &
113
726.8500000
BPVAL N2 OXYGEN -7.8000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO N2 .0374000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO .0374000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 N2 -.0315000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 CO2 -.0315000000 0.0 0.0 -273.1500000 726.8500000
BPVAL WATER METHANOL -.0789000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL WATER -.0789000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANOL .0148000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL CO2 .0148000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 METHANOL -.2881000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANOL N2 -.2881000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE H2 -.5100000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 BUTANE -.5100000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO H2 .0804000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO .0804000000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 H2 -.3426000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 CO2 -.3426000000 0.0 0.0 -273.1500000 726.8500000
BPVAL N2 H2 .0978000000 0.0 0.0 -273.1500000 726.8500000
BPVAL H2 N2 .0978000000 0.0 0.0 -273.1500000 726.8500000
BPVAL BUTANE METHANE 5.60000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE BUTANE 5.60000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO METHANE .0322000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO .0322000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 METHANE .0933000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE CO2 .0933000000 0.0 0.0 -273.1500000 &
114
726.8500000
BPVAL N2 METHANE .0278000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE N2 .0278000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 METHANE -.0222000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE H2 -.0222000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE PROPANE 0.0 0.0 0.0 -273.1500000 726.8500000
BPVAL PROPANE BUTANE 0.0 0.0 0.0 -273.1500000 726.8500000
BPVAL CO PROPANE .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE CO .0156000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL CO2 PROPANE .1289000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE CO2 .1289000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL N2 PROPANE .0763000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE N2 .0763000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 PROPANE -.2359000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE H2 -.2359000000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE PROPANE 9.00000000E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE METHANE 9.00000000E-3 0.0 0.0 -273.1500000 &
726.8500000
PROP-DATA SRKKIJ-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST SRKKIJ
115
BPVAL CO CO2 -.0154400000 0.0 0.0 -273.1500000 726.8500000
BPVAL CO2 CO -.0154400000 0.0 0.0 -273.1500000 726.8500000
BPVAL BUTANE METHANE .0226440000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE BUTANE .0226440000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 METHANE -.0244851000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE H2 -.0244851000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL BUTANE PROPANE -2.0759400E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE BUTANE -2.0759400E-3 0.0 0.0 -273.1500000 &
726.8500000
BPVAL H2 PROPANE .1014650000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE H2 .1014650000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL METHANE PROPANE .0241509000 0.0 0.0 -273.1500000 &
726.8500000
BPVAL PROPANE METHANE .0241509000 0.0 0.0 -273.1500000 &
726.8500000
PROP-DATA UNIQ-1
IN-UNITS ENG
PROP-LIST UNIQ
BPVAL WATER FORMIC 0.0 420.2459966 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL FORMIC WATER 0.0 278.9279978 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL WATER ACRYLIC 0.0 -815.2817335 0.0 0.0 212.7200023 &
248.9000020 0.0
BPVAL ACRYLIC WATER 0.0 455.6541564 0.0 0.0 212.7200023 &
248.9000020 0.0
BPVAL WATER THF -.3878309000 425.0131166 0.0 0.0 &
146.1380028 212.0000023 0.0
BPVAL THF WATER .3109718000 -1099.904031 0.0 0.0 &
146.1380028 212.0000023 0.0
BPVAL WATER BUTANOL -4.993400000 2824.291597 0.0 0.0 &
66.50600347 243.6800021 0.0
116
BPVAL BUTANOL WATER 3.764400000 -2603.900319 0.0 0.0 &
66.50600347 243.6800021 0.0
BPVAL ACRYLIC BUTANOL 0.0 572.3542754 0.0 0.0 248.0000020 &
284.0000017 0.0
BPVAL BUTANOL ACRYLIC 0.0 -616.4940551 0.0 0.0 248.0000020 &
284.0000017 0.0
BPVAL THF BUTANOL 0.0 -406.3535967 0.0 0.0 154.9400028 &
224.8700022 0.0
BPVAL BUTANOL THF 0.0 270.7903778 0.0 0.0 154.9400028 &
224.8700022 0.0
BPVAL WATER PROPANOL -2.333000000 1080.883071 0.0 0.0 &
77.00000338 212.0000023 0.0
BPVAL PROPANOL WATER 1.766800000 -1172.243151 0.0 0.0 &
77.00000338 212.0000023 0.0
BPVAL BUTANE PROPANOL 0.0 -273.6566978 0.0 0.0 50.00000360 &
104.0000032 0.0
BPVAL PROPANOL BUTANE 0.0 -60.55145952 0.0 0.0 50.00000360 &
104.0000032 0.0
BPVAL ACRYLIC PROPANOL 0.0 -1859.684385 0.0 0.0 &
212.0000023 284.0000017 0.0
BPVAL PROPANOL ACRYLIC 0.0 834.8853533 0.0 0.0 212.0000023 &
284.0000017 0.0
BPVAL THF PROPANOL 0.0 -483.8293761 0.0 0.0 150.4400028 &
207.3200023 0.0
BPVAL PROPANOL THF 0.0 310.2845375 0.0 0.0 150.4400028 &
207.3200023 0.0
BPVAL BUTANOL PROPANOL 0.0 53.83709957 0.0 0.0 104.0000032 &
243.6800021 0.0
BPVAL PROPANOL BUTANOL 0.0 -71.30987943 0.0 0.0 &
104.0000032 243.6800021 0.0
BPVAL WATER METHANOL .6437000000 -579.8361554 0.0 0.0 &
76.98200338 212.0000023 0.0
BPVAL METHANOL WATER -1.066200000 779.1812938 0.0 0.0 &
76.98200338 212.0000023 0.0
BPVAL BUTANE METHANOL 0.0 -1148.501691 0.0 0.0 122.0000030 &
122.0000030 0.0
BPVAL METHANOL BUTANE 0.0 -23.68817981 0.0 0.0 122.0000030 &
122.0000030 0.0
BPVAL THF METHANOL 0.0 -572.5058354 0.0 0.0 87.53000330 &
144.6800028 0.0
117
BPVAL METHANOL THF 0.0 161.6754587 0.0 0.0 87.53000330 &
144.6800028 0.0
BPVAL BUTANOL METHANOL .2267000000 -225.5174982 0.0 0.0 &
77.00000338 243.8960020 0.0
BPVAL METHANOL BUTANOL -.3136000000 148.7455188 0.0 0.0 &
77.00000338 243.8960020 0.0
BPVAL PROPANOL METHANOL 0.0 -167.8472987 0.0 0.0 &
140.0360029 206.8160023 0.0
BPVAL METHANOL PROPANOL 0.0 88.58789929 0.0 0.0 &
140.0360029 206.8160023 0.0
BPVAL WATER GAMMA-01 0.0 31.23053975 0.0 0.0 152.7800028 &
327.1640014 0.0
BPVAL GAMMA-01 WATER 0.0 -225.8560782 0.0 0.0 152.7800028 &
327.1640014 0.0
BPVAL THF GAMMA-01 -11.99890000 6474.853568 0.0 0.0 &
152.7440028 352.6160012 0.0
BPVAL GAMMA-01 THF 1.109300000 -207.5934583 0.0 0.0 &
152.7440028 352.6160012 0.0
BPVAL WATER 1:4-B-01 0.0 249.0355780 0.0 0.0 212.1800023 &
222.8000022 0.0
BPVAL 1:4-B-01 WATER 0.0 -1235.539610 0.0 0.0 212.1800023 &
222.8000022 0.0
BPVAL THF 1:4-B-01 2.601800000 -1934.671305 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL 1:4-B-01 THF -2.501400000 1594.517927 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL METHANOL 1:4-B-01 -.1912000000 383.7301169 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL 1:4-B-01 METHANOL .3393000000 -660.7933147 0.0 0.0 &
140.0000029 439.7000005 0.0
BPVAL WATER SUCCI-02 0.0 152.7533988 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL SUCCI-02 WATER 0.0 -15.60689988 0.0 0.0 68.00000346 &
104.0000032 0.0
BPVAL BUTANOL SUCCI-02 0.0 -251.2979980 0.0 0.0 &
68.00000346 104.0000032 0.0
BPVAL SUCCI-02 BUTANOL 0.0 181.7819985 0.0 0.0 68.00000346 &
104.0000032 0.0
PROP-DATA UNIQ-2
118
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST UNIQ 2
BPVAL WATER FORMIC 0.0 233.4700000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL FORMIC WATER 0.0 154.9600000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL WATER ACRYLIC 0.0 -452.9343000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL ACRYLIC WATER 0.0 253.1412000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL WATER THF -.3878309000 236.1184000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL THF WATER .3109718000 -611.0578000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL WATER BUTANOL -4.993400000 1569.050900 0.0 0.0 &
19.17000000 117.6000000 0.0
BPVAL BUTANOL WATER 3.764400000 -1446.611300 0.0 0.0 &
19.17000000 117.6000000 0.0
BPVAL ACRYLIC BUTANOL 0.0 317.9746000 0.0 0.0 120.0000000 &
140.0000000 0.0
BPVAL BUTANOL ACRYLIC 0.0 -342.4967000 0.0 0.0 120.0000000 &
140.0000000 0.0
BPVAL THF BUTANOL 0.0 -225.7520000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL BUTANOL THF 0.0 150.4391000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL WATER PROPANOL -2.333000000 600.4906000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL PROPANOL WATER 1.766800000 -651.2462000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL BUTANE PROPANOL 0.0 -152.0315000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL PROPANOL BUTANE 0.0 -33.63970000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL ACRYLIC PROPANOL 0.0 -1033.158000 0.0 0.0 &
119
100.0000000 140.0000000 0.0
BPVAL PROPANOL ACRYLIC 0.0 463.8252000 0.0 0.0 100.0000000 &
140.0000000 0.0
BPVAL THF PROPANOL 0.0 -268.7941000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL PROPANOL THF 0.0 172.3803000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL BUTANOL PROPANOL 0.0 29.90950000 0.0 0.0 40.00000000 &
117.6000000 0.0
BPVAL PROPANOL BUTANOL 0.0 -39.61660000 0.0 0.0 &
40.00000000 117.6000000 0.0
BPVAL WATER METHANOL .6437000000 -322.1312000 0.0 0.0 &
24.99000000 100.0000000 0.0
BPVAL METHANOL WATER -1.066200000 432.8785000 0.0 0.0 &
24.99000000 100.0000000 0.0
BPVAL BUTANE METHANOL 0.0 -638.0565000 0.0 0.0 50.00000000 &
50.00000000 0.0
BPVAL METHANOL BUTANE 0.0 -13.16010000 0.0 0.0 50.00000000 &
50.00000000 0.0
BPVAL THF METHANOL 0.0 -318.0588000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL METHANOL THF 0.0 89.81970000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL BUTANOL METHANOL .2267000000 -125.2875000 0.0 0.0 &
25.00000000 117.7200000 0.0
BPVAL METHANOL BUTANOL -.3136000000 82.63640000 0.0 0.0 &
25.00000000 117.7200000 0.0
BPVAL PROPANOL METHANOL 0.0 -93.24850000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL METHANOL PROPANOL 0.0 49.21550000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL WATER GAMMA-01 0.0 17.35030000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL GAMMA-01 WATER 0.0 -125.4756000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL THF GAMMA-01 -11.99890000 3597.140900 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL GAMMA-01 THF 1.109300000 -115.3297000 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL WATER 1:4-B-01 0.0 138.3531000 0.0 0.0 100.1000000 &
120
106.0000000 0.0
BPVAL 1:4-B-01 WATER 0.0 -686.4109000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL THF 1:4-B-01 2.601800000 -1074.817400 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 THF -2.501400000 885.8433000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL METHANOL 1:4-B-01 -.1912000000 213.1834000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 METHANOL .3393000000 -367.1074000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL WATER SUCCI-02 0.0 84.86300000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL SUCCI-02 WATER 0.0 -8.670500000 0.0 0.0 20.00000000 &
40.00000000 0.0
BPVAL BUTANOL SUCCI-02 0.0 -139.6100000 0.0 0.0 &
20.00000000 40.00000000 0.0
BPVAL SUCCI-02 BUTANOL 0.0 100.9900000 0.0 0.0 20.00000000 &
40.00000000 0.0
PROP-DATA WILSON-1
IN-UNITS MET VOLUME-FLOW='cum/hr' ENTHALPY-FLO='Gcal/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=Gcal MOLE-CONC='mol/l' &
PDROP=bar
PROP-LIST WILSON
BPVAL WATER ACRYLIC 0.0 168.4465000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL ACRYLIC WATER 0.0 -882.7916000 0.0 0.0 100.4000000 &
120.5000000 0.0
BPVAL WATER THF 1.166967000 -861.2151000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL THF WATER -9.570150000 2146.342000 0.0 0.0 &
63.41000000 100.0000000 0.0
BPVAL WATER BUTANOL .6102000000 -420.6027000 0.0 0.0 &
19.17000000 191.8000000 0.0
BPVAL BUTANOL WATER 2.450400000 -2492.023400 0.0 0.0 &
19.17000000 191.8000000 0.0
121
BPVAL THF BUTANOL 0.0 180.6092000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL BUTANOL THF 0.0 -388.8284000 0.0 0.0 68.30000000 &
107.1500000 0.0
BPVAL WATER PROPANOL 1.267500000 -580.1956000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL PROPANOL WATER -4.815800000 648.7817000 0.0 0.0 &
25.00000000 100.0000000 0.0
BPVAL BUTANE PROPANOL 0.0 -236.3575000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL PROPANOL BUTANE 0.0 -393.1257000 0.0 0.0 10.00000000 &
40.00000000 0.0
BPVAL THF PROPANOL 0.0 133.2163000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL PROPANOL THF 0.0 -299.9573000 0.0 0.0 65.80000000 &
97.40000000 0.0
BPVAL BUTANOL PROPANOL 0.0 -107.5577000 0.0 0.0 &
40.00000000 117.6000000 0.0
BPVAL PROPANOL BUTANOL 0.0 78.37730000 0.0 0.0 40.00000000 &
117.6000000 0.0
BPVAL WATER METHANOL -1.884200000 617.4097000 0.0 0.0 &
24.99000000 188.3000000 0.0
BPVAL METHANOL WATER 1.083700000 -580.2370000 0.0 0.0 &
24.99000000 188.3000000 0.0
BPVAL BUTANE METHANOL -.4811000000 -433.3017000 0.0 0.0 &
50.00000000 100.0000000 0.0
BPVAL METHANOL BUTANE 3.617800000 -1967.833100 0.0 0.0 &
50.00000000 100.0000000 0.0
BPVAL THF METHANOL 0.0 -95.32840000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL METHANOL THF 0.0 -201.7985000 0.0 0.0 30.85000000 &
62.60000000 0.0
BPVAL BUTANOL METHANOL -.6341000000 -73.65750000 0.0 0.0 &
25.00000000 285.4000000 0.0
BPVAL METHANOL BUTANOL .5587000000 -19.02890000 0.0 0.0 &
25.00000000 285.4000000 0.0
BPVAL PROPANOL METHANOL 0.0 -66.18770000 0.0 0.0 &
60.02000000 97.12000000 0.0
BPVAL METHANOL PROPANOL 0.0 47.93730000 0.0 0.0 &
60.02000000 97.12000000 0.0
122
BPVAL WATER GAMMA-01 0.0 -44.70750000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL GAMMA-01 WATER 0.0 -993.0518000 0.0 0.0 67.10000000 &
163.9800000 0.0
BPVAL THF GAMMA-01 -.2082000000 308.0572000 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL GAMMA-01 THF -30.94190000 10000.00000 0.0 0.0 &
67.08000000 178.1200000 0.0
BPVAL WATER 1:4-B-01 0.0 -506.5348000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL 1:4-B-01 WATER 0.0 -841.3055000 0.0 0.0 100.1000000 &
106.0000000 0.0
BPVAL THF 1:4-B-01 -7.241300000 2413.589800 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 THF 8.514000000 -3389.141600 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL METHANOL 1:4-B-01 -.1189000000 201.7588000 0.0 0.0 &
60.00000000 226.5000000 0.0
BPVAL 1:4-B-01 METHANOL -.5852000000 42.67770000 0.0 0.0 &
60.00000000 226.5000000 0.0
STREAM 36
SUBSTREAM MIXED TEMP=444. PRES=500.
MASS-FLOW WATER 1.621 / MAH 7627.813 / FORMIC 0.046 / &
ACRYLIC 18.448
STREAM 39
SUBSTREAM MIXED TEMP=70. PRES=3500. MASS-FLOW=858.233
MOLE-FLOW H2 1.
BLOCK M-201 MIXER
BLOCK S-201 FSPLIT
FRAC 47 0.95
BLOCK S-202 FSPLIT
FRAC 73 0.05
BLOCK E-201 HEATER
PARAM TEMP=464. PRES=614.7
123
BLOCK E-202 HEATER
PARAM TEMP=464. PRES=614.7
BLOCK E-203 HEATER
PARAM TEMP=40. <C> PRES=25. <bar>
BLOCK E-204 HEATER
PARAM TEMP=240. <C> PRES=600. <psig>
BLOCK E-205 HEATER
PARAM TEMP=80. <C> PRES=1. <bar>
BLOCK E-210 HEATER
PARAM TEMP=45. <C> PRES=1. <bar>
BLOCK E-211 HEATER
PARAM TEMP=96. PRES=14.7
BLOCK V-201 FLASH2
PARAM TEMP=40. <C> PRES=25. <bar>
BLOCK V-204 FLASH2
PARAM TEMP=45. <C> PRES=1. <bar>
BLOCK T-201 RADFRAC
PARAM NSTAGE=10 MAXOL=60
COL-CONFIG CONDENSER=PARTIAL-V
FEEDS 52 5 / 78 5
PRODUCTS 56 1 V / 60 10 L
P-SPEC 1 1. <bar> / 2 1. <bar>
COL-SPECS B:F=0.30222 MOLE-RR=2.
DB:F-PARAMS COMPS=THF
REPORT STDVPROF
BLOCK T-202 RADFRAC
PARAM NSTAGE=20 MAXOL=25
COL-CONFIG CONDENSER=PARTIAL-V
FEEDS 62 10
PRODUCTS 70 20 L / 66 1 V
124
P-SPEC 1 8. <bar> / 2 8. <bar>
COL-SPECS B:F=0.46366 MOLE-RR=3.
DB:F-PARAMS COMPS=WATER
REPORT STDVPROF
BLOCK R-201 RSTOIC
PARAM TEMP=240. <C> PRES=600. <psig> SERIES=YES
STOIC 1 MIXED MAH -1. / H2 -5. / THF 1. / WATER 2.
STOIC 2 MIXED MAH -1. / H2 -6. / BUTANOL 1. / WATER &
2.
STOIC 3 MIXED MAH -1. / H2 -3. / PROPANOL 1. / CO2 &
1.
STOIC 4 MIXED THF -1. / H2 -1.15 / BUTANE 0.15 / &
BUTANOL 0.85 / WATER 0.15
CONV 1 MIXED MAH 0.98
CONV 2 MIXED MAH 0.99
CONV 3 MIXED MAH 1.
CONV 4 MIXED THF 0.002
SELECTIVITY 1 THF MIXED MAH MIXED
BLOCK T-103P PUMP
PARAM PRES=614.7 EFF=0.8
BLOCK C-201 COMPR
PARAM TYPE=ASME-ISENTROP PRES=601.5 <psig> MEFF=0.85
BLOCK C-202 COMPR
PARAM TYPE=ASME-ISENTROP PRES=3. <bar> MEFF=0.85
BLOCK C-203 COMPR
PARAM TYPE=ASME-ISENTROP PRES=8.1 <bar> MEFF=0.85
BLOCK CV-201 VALVE
PARAM P-OUT=614.7
BLOCK CV-202 VALVE
PARAM P-OUT=16.
BLOCK CV-203 VALVE
PARAM P-OUT=14.7
125
BLOCK CV-204 VALVE
PARAM P-OUT=1.1 <bar>
EO-CONV-OPTI
CONV-OPTIONS
WEGSTEIN MAXIT=30
TEAR
TEAR 78 0.001 STATE=P
STREAM-REPOR MOLEFLOW MASSFLOW MASSFRAC
;
126
Appendix C – Material Saftey Data Sheet
Table C.1 has the material safety numbers for the National Fire Protection Association diamond
for the major components in the process. The products not included in this table are either not
hazardous or are present in such small quantity that a hazard is not prevalent.
Table C.1. NFPA values for major components.
Component Health Flammability Reactivity Special
Tetrahydrofuran 2 3 1
Maleic Anhydride 3 1 2
Butane 1 4 0
Maleic Acid 2 1 0
Formic Acid 3 2 2
Acrylic Acid 4 2 2
Hyrdogen 0 4 0 SA
Butanol 2 2 1 References 1, 4, 6, 8, 13, 14, 16, 18