1500 tpd ammonia production
TRANSCRIPT
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Natural Gas Composition (mol%)
Methane 92%
Ethane 2%
Propane 2%
Butane 1%Nitrogen 2%
Carbondioxide 1%
Total 100%
Pressure psig
Temperature F
Basis 4743 kgmo
Desired Production Rate 1500 Tonn
Stream Factor 345 days
Operating hours 8280 hour
Max. Hydrocarbon conc. in Steam r 0.50%
Steam to hydrocarbon ratio in Prim 3.3
Natural gas Flow rate 0
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Naphtha 4743
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Naptha composition (mol%) Naphtha
Carbon 46 100%
Hydrogen(H2) 53.9
Sulphur 0.17 8.06
Total 100
8.06
C H
l/hr Mixed Feed 46 53.9
s/day 1.17
552 108 5.44 665
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N.Gas
0%
551.8 108 5.44 665
6.65
6.65
6.649
Steam reforming
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Pre Reformer
Naphtha 4743
Temperature 763 K
Pressure psigPressure Drop psig
HC to Steam Ratio 3.5
Reaction 1 CnHm + n H2O ---> nCO + (2n+m)/2 H2
Reaction 2 CO + H2O --> CO2 + H2
Reaction 3 CO + 3H2--> CH4 + H2OSelectivity 100 mol CH4 / mol of CO2
Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)
Carbon 12 44.61479 2180.8314 26169.977
Hydrogen(H2) 2 52.25112 2554.1055 5108.211
Hydrogen gas 2 3.134097 153.19890 306.3978
Carbon monoxide 28 - - -
Carbon dioxide 44 - - -
Methane 16
Steam 18 - - -
Total 100 4888.1358 31584.58647.43
Steam Consumed 2193.57
Steam un reacted 6713.29
CO produced 2180.831
Components Mol. Wt
Stream 1 (Naphtha)
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Co consumed 1286.691
894.1409 0.00
CO 2 produced. 12.73951
Ch4 Produced 1273.951
Heat of
Formatio
ns A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225Propane 44 -104680 1.213 0.028785
Butane 58 -125790 1.935 0.036915
Nitrogen 28 0 3.28 0.000593
Carbon dioxide 44 -393509 5.457 0.001045
Carbon monoxide 28 -110525 3.376 0.000557
Hydrogen 2 0 3.249 0.000422
Oxygen 32 0 3.639 0.000506
Steam 18 -241818 3.47 0.00145
Naphtha 659.46 -1840303 - -
Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodat
edMethane 16 0.00% 0.00 0.00%
Ethane 30 0.00% 0.00 0.00%
Propane 44 0.00% 0.00 0.00%
Butane 58 0.00% 0.00 0.00%
Nitrogen 28 0.00% - 0.00%
Components Mol. Wt
Heat of Formations & Cp co
Components Mol. Wt
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Carbon dioxide 44 0.00% - 0.00%
Carbon monoxide 28 0.00% 0.00 0.00%
Hydrogen 2 3.13% 153.20 1.96%
Oxygen 32 0.00% 0.00 0.00%
Steam 18 0.00% 7632.91 97.44%Naphtha 659.46 0.00% 47.43 0.61%
7833.54 100.00%
KJ/Kmol Gjoules/hr
Del H specific -37716.9
Del H -3E+08 -295.457
Heat of Formation Summation -1933.06 rxn heat
Heat Supply required 0.024047
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Excess steam is used to ensure all naphtha converted
60% based on CO 0.59
100
Mol%
Mole
Flow
(mol/hr)
Mass
Flow
(kg/hr) Mol%
Mole
Flow
(kgmol/
hr)
Mass Flow
(kg/hr)
- - - - - -
- - - - - -
- - - 10.82 1079.02 2158.04
- - - 8.97 894.14 25035.94
- - - 0.13 12.74 560.54
12.77 1273.95 20383.22
100 7632.91 1E+05 67.31 6713.29 120839.2201
100 7632.91 1E+05 100 9973.14 168976.960.00
Stream 2 (Steam) Stream 3(Raw syn gas)
Pre reformer
1
2 3
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C D
-0 0 API Gravit 74.7682
-0 0 Sp. Gravity 0.686-0 0 Heating val 17924.2 BTU/Lb
-0 0 41602 J/kg
0 4000 27434.8 kj/mol
0 -115700 n m
0 -3100 45.98 53.85
0 8300 M.wat 659.46
0 -22700 Heat of Formation -1840303.279
0 12100
- -
T
initial T final Tau Cp H 0 f 1036 298.00 0.288 55.6878 0 0.00
1036 298.00 0.288 93.3467 0 0.00
1036 298.00 0.288 133.742 0 0.00
1036 298.00 0.288 174.321 0 0.00
1036 298.00 0.288 30.5673 0 0.00
fficients
Pre- Reformer Inlet
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1036 298.00 0.288 50.9067 0 0.00
1036 298.00 0.288 31.15 0 0.00
1036 298.00 0.288 29.3709 0.5744 0.00
1036 298.00 0.288 33.0101 0 0.00
1036 298.00 0.288 36.9174 35.9719 -235624.671405 77.00 - 2404.84 14.5607 -11142.55
51.107 -246767.22
763 1405.4
763
110.9
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H2 for Hyderotreating ( 161.3 kgmol/hr
#####
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Mol%
Mole
Flow
(kgmol/hr
)
Mol%
accomod
ated
T
initial T final Tau Cp 0.00% 1273.95 12.77% 298 783.00 2.628 49.35 6.304
0.00% 0.00 0.00% 298 783.00 2.628 81.38 0
0.00% 0.00 0.00% 298 783.00 2.628 116.6 0
0.00% 0.00 0.00% 298 783.00 2.628 152.4 0
0.00% 0.00 0.00% 298 783.00 2.628 30.92 0
Pre-Reformer Outlet
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0.00% 12.74 0.13% 298 783.00 2.628 21.6 0.028
0.00% 894.14 8.97% 298 783.00 2.628 29.81 2.672
100.00% 1079.02 10.82% 298 783.00 2.628 30.95 3.349
0.00% 0.00% 298 783.00 2.628 26.94 0
100.00% 6713.29 67.31% 298 783.00 2.628 38.34 25.81
200.00% 9973.14 100.00% 38.16
KJ/Kmol joules/hr 510.00 Temp C
Del H spe 18508.49
Del H 1.85E+08 184.588 Heat Exchange from Flue Ga
Heat of Formation Su -1822.17 0.02405
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H 0 f Mol%
Mole
Flow
(kgmol/h
r)
Mol%
accomo
dated
T
initial T final Tau-9519.05 0.00% 1273.95 12.77% 783.00 973.00 1.243
0.00 0.00% 0.00 0.00% 783 973.00 1.243
0.00 0.00% 0.00 0.00% 783 973.00 1.243
0.00 0.00% 0.00 0.00% 783 973.00 1.243
0.00 0.00% 0.00 0.00% 783 973.00 1.243
Stream 10 (SR OUTLET) Heat Exchange fro
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-502.66 0.00% 12.74 0.13% 783 973.00 1.243
-9909.10 0.00% 894.14 8.97% 783 973.00 1.243
0.00 0.00% 1079.02 10.82% 783 973.00 1.243
0.00 0.00% 0.00 0.00% 783 973.00 1.243
-162776.59 0.00% 6713.29 67.31% 783 973.00 1.2430.00
-182707.41 0.00% 9973.14 100.00%
KJ/Kmol Gjoules/hr
Del H s 7864.26
Convection Del H 7.8E+07 78.4313
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Cp H 0 f 66.52 8.497 -9519.05
114 0 0.00
163.4 0 0.00
212.2 0 0.00
31.67 0 0.00
Convection section
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51.05 0.065 -502.66
32.08 2.876 -9909.10
30.23 3.271 0.00
33.57 0 0.00
39.64 26.68 -162776.590.00
41.39 -182707.41
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N.Gas Naphtha
Primary Reformer Inlet 0% 100.0%
Primary Reformer Outlet
Temperature 700 C Temperature 750
Pressure 575 psig Pressure 575
Pressure Drop 10 psig Pressure Drop 10
HC to Steam Ratio 3 HC to Steam Ratio 3N.Gas Flow rate 0
Mixed with N.Gas
Steam
Reactions in Primary Reformer
Reaction 1 CH4 + H2O = CO + 3H2 75%
Reaction 2 C2H6 + 2H2O = 2CO + 5H2 100%
Reaction 3 C3H8 + 3H2O = 3CO + 7H2 100%
Reaction 4 C4H10 + 4H2O = 4CO + 9H2 100%Reaction 5 CO+H2O = CO2 + H2 40%
Mol% Mole Flow (kgmol/hr)
Mass Flow
(kg/hr)
Methane 16 12.77381594 1273.95 20383.21625
Ethane 30 0 0 0
Propane 44 0 0 0
Butane 58 0 0 0
Nitrogen 28 0 0 0Carbon dioxide 44 0.127738159 12.73951016 560.538447
Carbon monoxide 28 8.965486749 894.14 25035.94447
Hydrogen 2 10.81927924 1079.02 2158.044525
Oxygen 32 - - -
Steam 18 67.31367991 6713.29 120839.2201
Argon 40 - - -
Total 100 9973.14 168976.9638
Total Primary Reformer Inlet 165214.7057 kg/hr
CO Production Del H Rxn
Reaction 1 955.46 kgmol/hr 1.96647E+11
Reaction 2 0 kgmol/hr 0
Reaction 3 0 kgmol/hr 0
Reaction 4 0 kgmol/hr 0
Total 1849.60
CO Consume
Components Mol. Wt
Stream 4 (Mixed stream withNatural Gas)
4
5
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Reaction 5 739.841654 kgmol/hr -30456321543
CO2 Produced
Reaction 5 739.841654 kgmol/hr
H2 Produced
Reaction 1 2866.38979 kgmol/hrReaction 2 0 kgmol/hr
Reaction 3 0 kgmol/hr
Reaction 4 0 kgmol/hr
Reaction 5 739.841654 kgmol/hr
Total 4685.25 kgmol/hr
Steam consumption
Reaction 1 955.463262 kgmol/hr
Reaction 2 0 kgmol/hr
Reaction 3 0 kgmol/hr
Reaction 4 0 kgmol/hr Reaction 5 739.841654 kgmol/hr
Total 1695.30492 kgmol/hr
1.6619E+11 166.1904388
Equilibrium Shift Conversion
1849.60 Keq 0.74654.67 6504.28 Conv. 37.43%
CO H20 CO2 H2
1849.60 4654.67 12.73951016 3945.41
a b c
-0.3 -8498.41 6026509.804
CO conc eqlib 17412.14 CO conc. Eq -415.3315507
-29020.236 692.2192511
Heat ofFormations A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225
Propane 44 -104680 1.213 0.028785
Butane 58 -125790 1.935 0.036915
Nitrogen 28 0 3.28 0.000593
Carbon dioxide 44 -393509 5.457 0.001045
Carbon monoxide 28 -110525 3.376 0.000557
Components Mol. Wt
Heat of Formations & Cp coe
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Hydrogen 2 0 3.249 0.000422
Oxygen 32 0 3.639 0.000506
Steam 18 -241818 3.47 0.00145
Mol% Mole Flow (kgmol/hr)
Mol%
accomodated
Methane 16 12.77% 1273.95 13.05%
Ethane 30 0.00% 0.00 0.00%
Propane 44 0.00% 0.00 0.00%
Butane 58 0.00% 0.00 0.00%
Nitrogen 28 0.00% 0.00 0.00%
Carbon dioxide 44 0.13% 12.74 0.13%
Carbon monoxide 28 8.97% 894.14 9.16%
Hydrogen 2 10.82% 1079.02 11.05%
Oxygen 32 0.00% 0.00 0.00%
Steam 18 67.31% 6504.28 66.61%
100.00% 9764.13
KJ/Kmol Gjoules/hr
Del H specific -25346.966Del H -247491055 -247.491055
Heat of Formation Summation -1771.6238
Heat Supply required 245.3708166
3.926253962 Gjoules per ton Ammonia
Compressor Section Pin T in Pout
14.7 298 589.7
Gamma 1.43
r-1/r 0.3006993
Pre Heating Air required Tin Tf Del H required
904 1023.00
M.Wt Mol % mol%
Oxygen 32 21.00% 510.74 21.00%Nitrogen 28 79.00% 1921.37 79.00%
2432.11
KJ/Kmol Gjoules/hr
Del H specific 3854.43525
Del H 9374411.56 9.374411561
Heat of Formations & Cp coe
Components Mol. Wt
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Heat of
Formations A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225
Propane 44 -104680 1.213 0.028785
Butane 58 -125790 1.935 0.036915
Nitrogen 28 0 3.28 0.000593Carbon dioxide 44 -393509 5.457 0.001045
Carbon monoxide 28 -110525 3.376 0.000557
Hydrogen 2 0 3.249 0.000422
Oxygen 32 0 3.639 0.000506
Steam 18 -241818 3.47 0.00145
Mol% Mole Flow (kgmol/hr)
Mol%
accomodate
dMethane 16 2.73% 38.22 0.28%
Ethane 30 0.00% 0.00 0.00%
Propane 44 0.00% 0.00 0.00%
Butane 58 0.00% 0.00 0.00%
Nitrogen 28 0.00% 1921.37 13.90%
Carbon dioxide 44 6.45% 752.58 5.44%
Carbon monoxide 28 9.51% 1109.76 8.03%
Hydrogen 2 40.13% 4685.25 33.89%
Oxygen 32 0.00% 510.74 0.00%
Steam 18 41.19% 4808.97 34.78%
100.00% 13826.90
KJ/Kmol Gjoules/hr
Del H specific -23503.703Del H -324983283 -324.983283
Heat of Formation Summation -1584.54769
Heat Requirement 15.24551817 reax
60% Heat Provided
Heat of Combustion required 408.951361 GJ/hr
Heating value Of Fuel 8015 kcal/m3
0.03355079 Gjoules/m3
Fuel required 12189.0233 m3
195.0403136 m3/ TonAmm
Furnace Firing Fuel Consumption
Components Mol. Wt
Components Mol. Wt
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Naphtha
Heating value Of Fuel 10556 kcal/kg
44187.416 Kj/kg
0.044187416 Gj/kg
Fuel required 9254.928168 kg/hr
9.254928168 Tons/hr
0.148090954 Tons/Ton Am
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Secondary Reformer
C
psig Exit Temperature 1200.80 C
psig Pressure 565 psig
Pressure Drop 10 psig
Air
Reactions in Secondary
based CH4 205813 Reaction 1 CH4 + H2O = CO +
based C2H6 3464061 Reaction 2 CH4 + 2O2 = CO2 +
based C3H8 498559 Reaction 3 2CO + O2 = 2CO
based C4H10 650962 Reaction 4 2CO + 2.5O2 +H2= 2CObased on CO -41166
Mol%
Mole Flow
(mol/hr)
Mass Flow
(kg/hr) Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)
- - - 2.73 318.49 5095.80
- - - 0.00 0.00 0.00
- - - 0.00 0.00 0.00
- - - 0.00 0.00 0.00
- - - 0.00 0.00 0.00- - - 6.45 752.58 33113.57
- - - 9.51 1109.76 31073.35
- - - 40.13 4685.25 9370.51
- - - - - -
100 -209.014336 -3762.25805 41.19 4808.97 86561.47356
100 -209.014336 -3762.25805 100 11675.05586 165214.7057
Total Secondary Reformer Inlet
Total Secondary Reformer Outlet
Nitrogen in 1921.37 kgmol/hr
Total air 2432.11 kgmol/hr
O2 with Air 510.74 kgmol/hr
Argon with Air 0.00 kgmol/hr
CH4 Consumption
Reaction 2 63.70 kgmol/hr
Reaction 1 216.57 kgmol/hr
Stream 5 (Steam) Stream 6
Primary ReformerSecondary
Reformer
7
6 8
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CO Production
Reaction 1 216.57 kgmol/hr
CO Consumption
Reaction 4 511.13 kgmol/hr
CO2 ProductionReaction 2 63.70 kgmol/hr
Reaction 4 511.13
H2 production
Reaction 1 649.72 kgmol/hr
H2 Consumed
Reaction4 255.57 kgmol/hr
Steam Consumption
1800 1192 1474 Reaction 1 216.57 kgmol/hr
982.2222222 644.4444444 801.1111111
Steam Production
Reaction 4 255.57 kgmol/hrReaction 2 127.40
O2 Consumption
GJ Reaction 2 127.40
Reaction 4 383.35
C D
-0.000002164 0
-0.000005561 0
-0.000008824 0
-0.000011402 0
0 4000
0 -115700
0 -3100
fficients
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0 8300
0 -22700
0 12100
T initial T final Tau Cp H 0 f
973 298.00 0.30626927 54.18115362 7.069154181 -9722.82
973 298.00 0.30626927 90.55173505 0 0.00
973 298.00 0.30626927 129.7579981 0 0.00
973 298.00 0.30626927 169.2460049 0 0.00
973 298.00 0.30626927 30.41382177 0 0.00
973 298.00 0.30626927 50.57961785 0.065992526 -513.42
973 298.00 0.30626927 31.00266192 2.839039333 -10121.22
973 298.00 0.30626927 29.26416652 3.233948066 0.00
973 298.00 0.30626927 32.86706685 0 0.00
973 298.00 0.30626927 36.54326732 24.34292669 -161084.61
37.55106079 -181442.07
Tout
904 K
631 0C
Tin T required Tau Cp
904 1023.00 1.131212078 34.04764749 7.150005973 0.00904 1023.00 1.131212078 32.0670063 25.33293498 0.00
Cp 32.48294095
fficients
Primary Reformer Inlet
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C D
-0.000002164 0
-0.000005561 0
-0.000008824 0
-0.000011402 0
0 40000 -115700
0 -3100
0 8300
0 -22700
0 12100
T initial T final Tau Cp H 0 f 1023.00 298.00 0.291300098 55.38076461 0.153076388 -205.98
1023.00 298.00 0.291300098 92.77996548 0 0.00
1023 298.00 0.291300098 132.9360584 0 0.00
1023 298.00 0.291300098 173.2944119 0 0.00
1023 298.00 0.291300098 30.53557519 4.243182714 0.00
1023 298.00 0.291300098 50.84025585 2.76717323 -21418.22
1023 298.00 0.291300098 31.11959813 2.497694363 -8870.86
1023 298.00 0.291300098 29.34876333 9.944849017 0.00
1023 298.00 0.291300098 32.98076072 0 0.00
1023 298.00 0.291300098 36.84010737 12.81292543 -84103.88
32.41890114 -114598.94
-233.8797714 Gj/hr
by Radiation
nia
Secondary Reformer Inlet
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onia
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Ammonia Productio 62.49489181 TPH
39.62414966
Reformer
3H2 85% based on remaining CH4 after Reaction 4
H2O 20%
2
2 + H2O 100% based on O2
Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%
Mole Flow
(kgmol/hr)
- - - 0.27 38.22
- - - - -
- - - - -
- - - - -
79 1921.37 53798.27914 13.57 1921.37- - - 9.38 1327.41
- - - 5.76 815.20
- - - 35.88 5079.40
21 510.74 16343.78 0.00 0.00
- - 35.14 4975.36
0 0
100 2432.11 70142.06 100 14156.96
235356.77 kg/hr
235356.77 kg/hr
N2:H2 Ratio 3.0000379 3
2.4385 0.999987356
2.438469167
2.4577876 For mix feed
2.462481 For 100% n.gas
2.4385 For 100% naphtha
Stream 7 (Air) Stream 8
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Mol%Mole Flow(kgmol/hr)
Mol%accomodated T initial T final
2.73% 38.22 2.73% 298 1023.00
0.00% 0.00 0.00% 298 1023.00
0.00% 0.00 0.00% 298 1023.00
0.00% 0.00 0.00% 298 1023.00
0.00% 0.00 0.00% 298 1023.00
6.45% 752.58 6.45% 298 1023.00
9.51% 1109.76 9.51% 298 1023.00
40.13% 4685.25 40.13% 298 1023.00
0.00% - 0.00% 298 1023.00
41.19% 4808.97 41.19% 298 1023.00
100.00% 11394.79
KJ/Kmol Gjoules/hr
Del H specific 25286.27402Del H 288131697.2 288.1316972
Heat of Formation Summation -1566.893622
Primary Reformer Outlet
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Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodated T initial T final0.00% 38.22 0.27% 298 1473.80
0.00% 0.00 0.00% 298 1473.80
0.00% 0.00 0.00% 298 1473.80
0.00% 0.00 0.00% 298 1473.80
0.00% 1921.37 13.57% 298 1473.80
0.00% 1327.41 9.38% 298 1473.80
0.00% 815.20 5.76% 298 1473.80
0.00% 5079.40 35.88% 298 1473.80
0.00% 0.00 0.00% 298 1473.80
0.00% 4975.36 35.14% 298 1473.80
0.00% 14156.96
1200.80
KJ/Kmol Gjoules/hr
Del H specific 40553.09296Del H 574108572.3 574.1085723
Heat of Formation Summation -1818.427466 15.24551817
Secondary Reformer Outlet
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Mass Flow
(kg/hr) Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)
611.50 92% 0.00 0
- 2% 0.00 0
- 2% 0.00 0
- 1% 0.00 0
53798.28 2% 0.00 058406.02 1% 0.00 0
22825.70 0 0.00 0
10158.81 0 0.00 0
0.00 0 - -
89556.47 0 0.00 0
0 - -
235356.77 100.00% 0.00 0
168976.96
0.00
0.00
Natural Gas
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Tau Cp H 0 f
3.432885906 55.38076461 1.510750402 -2032.86
3.432885906 92.77996548 0 0.00
3.432885906 132.9360584 0 0.00
3.432885906 173.2944119 0 0.00
3.432885906 31.81189175 0 0.00
3.432885906 13.92279939 0.897472073 -25365.83
3.432885906 30.1304528 2.864024505 -10505.86
3.432885906 31.99712019 12.84059174 0.00
3.432885906 25.73766425 0 0.00
3.432885906 40.70096496 16.76478062 -99605.15
34.87761934 -137509.69
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Tau Cp H 0 f 4.945637584 64.84253338 0.175050723 -201.18
4.945637584 109.390407 0 0.00
4.945637584 156.0686441 0 0.00
4.945637584 202.6610967 0 0.00
4.945637584 33.48966608 4.545180361 0.00
4.945637584 -0.50510527 -0.04736055 -36896.87
4.945637584 30.73521444 1.769832595 -6364.39
4.945637584 33.9634395 12.18580763 0.00
4.945637584 23.47096982 0 0.00
4.945637584 45.13191265 15.86127744 -84985.15
34.48978819 -128447.58
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High Temperature Shift Converter
Temperature 315 C 599
Pressure 565 psig 38.43537415
Pressure Drop 10 psig
SR outlet stream
Reactions in HTS
Reaction 1 CO+H2O = CO2 + H2 80% based on CO
Mol%Mole Flow(kgmol/hr)
Mass Flow(kg/hr) Mol%
Methane 16 0.27 38.22 611.50 0.27
Nitrogen 28 13.57 1921.37 53798.28 13.57
Carbon dioxide 44 9.38 1327.41 58406.02 13.98
Carbon monoxide 28 5.76 815.20 22825.70 1.15
Hydrogen 2 35.88 5079.40 10158.81 40.49
Steam 18 35.14 4975.36 89556.47 30.54Total 100 14157.0 235356.8 100
CO Consume
Reaction 1 652.16 kgmol/hr CO2 Produced
Reaction 1 652.16 kgmol/hr
H2 Produced
Reaction 1 652.16 kgmol/hr
Steam Consume
Reaction 1 652.16 kgmol/hr
Formations A B C
Methane 16 -74520 1.702 0.009081 -2.164E-06
Ethane 30 -83820 1.131 0.019225 -5.561E-06
Propane 44 -104680 1.213 0.028785 -8.824E-06
Butane 58 -125790 1.935 0.036915 -1.1402E-05
Components Mol. Wt
Stream 9 (SR outlet) Stre
Components Mol. WtHeat of Formations & Cp coefficients
HTS9
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Nitrogen 28 0 3.28 0.000593 0
Carbon dioxide 44 -393509 5.457 0.001045 0
Carbon monoxide 28 -110525 3.376 0.000557 0
Hydrogen 2 0 3.249 0.000422 0
Oxygen 32 0 3.639 0.000506 0
Steam 18 -241818 3.47 0.00145 0
Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodate
d T initial
Methane 16 0.27% 38.22 0.27% 1473.80
Ethane 30 0.00% 0.00 0.00% 1473.8
Propane 44 0.00% 0.00 0.00% 1473.8
Butane 58 0.00% 0.00 0.00% 1473.8
Nitrogen 28 13.57% 1921.37 13.57% 1473.8
Carbon dioxide 44 9.38% 1327.41 9.38% 1473.8
Carbon monoxide 28 5.76% 815.20 5.76% 1473.8
Hydrogen 2 35.88% 5079.40 35.88% 1473.8
Oxygen 32 0.00% 0.00 0.00% 1473.8
Steam 18 35.14% 4975.36 35.14% 1473.8
100.00% 14156.96
315
KJ/Kmol Gjoules/hr 1200.8
Del H specific -32828.16852Del H -464747115 -464.747115
Heat of Formation Summation 0 rxn heat 0
Heat Supply required -464.747115
Heat of
Formations A B C
Methane 16 -74520 1.702 0.009081 -2.164E-06
Ethane 30 -83820 1.131 0.019225 -5.561E-06Propane 44 -104680 1.213 0.028785 -8.824E-06
Butane 58 -125790 1.935 0.036915 -1.1402E-05
Nitrogen 28 0 3.28 0.000593 0
Carbon dioxide 44 -393509 5.457 0.001045 0Carbon monoxide 28 -110525 3.376 0.000557 0Hydrogen 2 0 3.249 0.000422 0
Oxygen 32 0 3.639 0.000506 0
Steam 18 -241818 3.47 0.00145 0
Components Mol. Wt
Heat of Formations & Cp coefficients
Components Mol. Wt
Stream 9 (SR Inlet)
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Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodate
d T initial
Methane 16 0.27% 38.22 0.27% 588
Ethane 30 0.00% 0.00 0.00% 588Propane 44 0.00% 0.00 0.00% 588
Butane 58 0.00% 0.00 0.00% 588
Nitrogen 28 13.57% 1921.37 13.57% 588
Carbon dioxide 44 9.38% 1327.41 9.38% 588
Carbon monoxide 28 5.76% 815.20 5.76% 588
Hydrogen 2 35.88% 5079.40 35.88% 588
Oxygen 32 0.00% 0.00 0.00% 588
Steam 18 35.14% 4975.36 35.14% 588
100.00% 14156.96
315
KJ/Kmol Gjoules/hr 315
Del H specific -9480.381971Del H -134213401.8 -134.213402
Heat of Formation Summation -1818.42747 rxn heat -26.846931
Heat Supply required -0.48060121
Heat of
Formations A B C
Methane 16 -74520 1.702 0.009081 -2.164E-06
Ethane 30 -83820 1.131 0.019225 -5.561E-06Propane 44 -104680 1.213 0.028785 -8.824E-06
Butane 58 -125790 1.935 0.036915 -1.1402E-05
Nitrogen 28 0 3.28 0.000593 0
Carbon dioxide 44 -393509 5.457 0.001045 0
Carbon monoxide 28 -110525 3.376 0.000557 0
Hydrogen 2 0 3.249 0.000422 0
Oxygen 32 0 3.639 0.000506 0
Steam 18 -241818 3.47 0.00145 0
Mol%
Mole Flow
(kgmol/hr)
Mol%accomodate
d T initial
Methane 16 0.27% 38.22 0.27% 543
Ethane 30 0.00% 0.00 0.00% 543
Propane 44 0.00% 0.00 0.00% 543
Butane 58 0.00% 0.00 0.00% 543
Nitrogen 28 13.57% 1921.37 13.57% 543
Components Mol. Wt
Components Mol. Wt
Strea
Components Mol. Wt
Heat of Formations & Cp coefficients
St
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Carbon dioxide 44 13.98% 1979.57 13.98% 543
Carbon monoxide 28 1.15% 163.04 1.15% 543
Hydrogen 2 40.49% 5731.57 40.49% 543
Oxygen 32 0.00% 0.00 0.00% 543
Steam 18 30.54% 4323.20 30.54% 543
100.00% 14156.96
270KJ/Kmol Gjoules/hr 270
Del H specific -8098.750514Del H -114653698.5 -114.653699
Heat of Formation Summation -1845.2744 rxn heat -5.3693862
Heat Supply required -1.20079189
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Low Temperature Shift converter
Exit Temperature 200 C
Pressure 555 psig
Pressure Drop 10 psig
Reactions in LTS
Reaction 1 CO+H2O = CO2 + H2 80% based on CO
Mole Flow(kgmol/hr)
Mass Flow(kg/hr) Mol%
Mole Flow(kgmol/hr)
Mass Flow(kg/hr)
38.22 611.50 0.27 38.22 611.50
1921.37 53798.28 13.57 1921.37 53798.28
1979.57 87101.18 14.90 2110.00 92840.21
163.04 4565.14 0.23 32.61 913.03
5731.57 11463.13 41.41 5862.00 11724.00
4323.20 77817.54 29.62 4192.76 75469.75693
14156.96 235356.77 100 14156.96 235356.77
CO Consume
Reaction 1 130.43 kgmol/hrCO2 Produced
Reaction 1 130.43 kgmol/hr
H2 Produced
Reaction 1 130.43 kgmol/hr
Steam Consume
Reaction 1 130.43 kgmol/hr
D
0
0
0
0
m 10 (HTS outlet) Stream 11(LTS outlet)
LTS
10 11
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4000
-115700
-3100
8300
-22700
12100
T final Tau Cp H 0 f
588.00 0.398968652 71.68583919 0.193525104 -201.18
588.00 0.398968652 122.0200634 0 0.00
588.00 0.398968652 174.034758 0 0.00
588.00 0.398968652 225.5388899 0 0.00
588.00 0.398968652 32.3585737 4.391669757 0.00
588.00 0.398968652 54.14940403 5.077249898 -36896.87
588.00 0.398968652 32.83732269 1.890878756 -6364.39
588.00 0.398968652 30.64178195 10.99402374 0.00
588.00 0.398968652 34.55685721 0 0.00
588.00 0.398968652 41.29586686 14.51312747 -84985.15
37.06047473 -128447.58
599
D
0
00
0
4000
-115700
-3100
8300
-22700
12100
Cool down to reactor Inlet temp
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T final Tau Cp H 0 f Mol%
Mole Flow
(kgmol/hr)
298.00 0.506802721 43.93977376 0.118621047 -201.18 0.27% 38.22
298.00 0.506802721 70.8133391 0 0.00 0.00% 0.00298.00 0.506802721 101.191459 0 0.00 0.00% 0.00
298.00 0.506802721 132.7812718 0 0.00 0.00% 0.00
298.00 0.506802721 29.5027472 4.004080151 0.00 13.57% 1921.37
298.00 0.506802721 47.80831182 4.482685464 -36896.87 13.98% 1979.57
298.00 0.506802721 30.08177233 1.732205295 -6364.39 1.15% 163.04
298.00 0.506802721 28.66760656 10.28570557 0.00 40.49% 5731.57
298.00 0.506802721 31.84165231 0 0.00 0.00% 0.00
298.00 0.506802721 34.33753975 12.06767479 -84985.15 30.54% 4323.20
32.69097231 -128447.58 100.00% 14156.96
599
KJ/Kmol
Del H specif 11342.81057Del H 160579731.6
Heat of Formation Summatio
D
0
00
0
4000
-115700
-3100
8300
-22700
12100
T final Tau Cp H 0 f Mol%
Mole Flow
(kgmol/hr)
298.00 0.548802947 42.62668421 0.115076193 -201.18 0.27% 38.22
298.00 0.548802947 68.20804357 0 0.00 0.00% 0.00
298.00 0.548802947 97.37932321 0 0.00 0.00% 0.00
298.00 0.548802947 127.9077245 0 0.00 0.00% 0.00
298.00 0.548802947 29.40496939 3.990809854 0.00 13.57% 1921.37
m 10 (HTSC outlet)
eam 9 (SR Inlet)
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298.00 0.548802947 47.23241509 6.604522854 -55024.48 14.90% 2110.00
298.00 0.548802947 29.96738454 0.345123695 -1272.88 0.23% 32.61
298.00 0.548802947 28.61595497 11.58541244 0.00 41.41% 5862.00
298.00 0.548802947 31.67236135 0 0.00 0.00% 0.00
298.00 0.548802947 34.10607948 10.41517951 -73845.42 29.62% 4192.76
33.05612455 -130343.96 100.00% 14156.96
518KJ/Kmol
Del H specif 8393.205954Del H 118822292.8
Heat of Formation Summatio
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Mol%
accomodate
d T initial T final Tau Cp H 0 f
0.27% 298 654.48 2.196241611 45.83519859 0.123737989 -201.18
0.00% 298 654.48 2.196241611 74.54801233 0 0.000.00% 298 654.48 2.196241611 106.6420192 0 0.00
0.00% 298 654.48 2.196241611 139.7469414 0 0.00
13.57% 298 654.48 2.196241611 30.44034473 4.131329847 0.00
13.98% 298 654.48 2.196241611 25.71732341 3.596061093 -55024.48
1.15% 298 654.48 2.196241611 29.63607223 0.34130809 -1272.88
40.49% 298 654.48 2.196241611 30.38969341 12.30352551 0.00
0.00% 298 654.48 2.196241611 27.5906417 0 0.00
30.54% 298 654.48 2.196241611 37.07875369 11.32296298 -73845.42
31.81892552 -130343.96
Gjoules/hr 381.48 Temp C
160.5797316
-1845.2744 -0.48060121
Mol%accomodate
d T initial T final Tau Cp H 0 f
0.27% 298 563.00 1.889261745 43.21327815 0.116659779 -201.18
0.00% 298 563.00 1.889261745 69.37365838 0 0.00
0.00% 298 563.00 1.889261745 99.0858329 0 0.00
0.00% 298 563.00 1.889261745 130.0895449 0 0.00
13.57% 298 563.00 1.889261745 30.09987713 4.085121961 0.00
LTSC Stream 11 (LTSC OUT)
Stream 10 (SR OUTLET)
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14.90% 298 563.00 1.889261745 28.64515109 4.269376924 -58650.00
0.23% 298 563.00 1.889261745 29.51334909 0.067978946 -254.58
41.41% 298 563.00 1.889261745 29.99067191 12.41829178 0.00
0.00% 298 563.00 1.889261745 28.05061776 0 0.00
29.62% 298 563.00 1.889261745 36.17958977 10.71504591 -71617.48
31.6724753 -130723.23
Gjoules/hr 290.00 Temp C
118.8222928
-1850.64378 -1.20079189
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Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodate
d T initial T final Tau Cp
0.27% 38.22 0.27% 654.48 543.00 0.8296663 52.88656225
0.00% 0.00 0.00% 654.48 543.00 0.8296663 88.481384660.00% 0.00 0.00% 654.48 543.00 0.8296663 126.9986797
0.00% 0.00 0.00% 654.48 543.00 0.8296663 165.7660314
13.57% 1921.37 13.57% 654.48 543.00 0.8296663 30.28624321
13.98% 1979.57 13.98% 654.48 543.00 0.8296663 48.70825215
1.15% 163.04 1.15% 654.48 543.00 0.8296663 30.79084697
40.49% 5731.57 40.49% 654.48 543.00 0.8296663 29.24652926
0.00% 0.00 0.00% 654.48 543.00 0.8296663 32.40792591
30.54% 4323.20 30.54% 654.48 543.00 0.8296663 36.26242287
100.00% 14156.96
KJ/Kmol Gjoules/hr
Del H specifi -3827.45032Del H -54185066.6 -54.1850666 Heat Surplus
Heat of Formation Summatio -1845.2744
COOL Down HTSC OUTLET
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H 0 f
0.142774048 -201.18
0 0.000 0.00
0 0.00
4.11041536 0.00
6.810889596 -55024.48
0.354607219 -1272.88
11.8407058 0.00
0 0.00
11.07367511 -73845.42
34.33306713 -130343.96
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Cooler Separator
Temperature C
Pressure 555 psig LTS outlet stream
Pressure Drop psig
Assumptions:
Water Condensed 100%
CO2 Solubility in Water 0%
Mol%
Mole Flow
(kgmol/hr) Mass Flow (kg/hr)
Methane 16 0.27 38.22 611.50
Nitrogen 28 13.57 1921.37 53798.28
Carbon dioxide 44 14.90 2110.00 92840.21
Carbon monoxide 28 0.23 32.61 913.03Hydrogen 2 41.41 5862.00 11724.00
Steam 18 29.62 4192.76 75469.76
Total 100 14157.0 235356.8
CO2 Removal
Temperature C Stream from
Pressure 555 psig Cooler Separator
Pressure Drop 10 psig
Lean Solvent
Assumptions:
Solvent Used MDEA
Rich Solvent Loading 0.55 mol of Acid gas /mol of pure solvent
Lean Solvent Loading 0.10 mol of Acid gas /mol of pure solvent
Solution Strength 50% by weight
Mol%
Mole Flow
(kgmol/hr) Mass Flow (kg/hr)
Methane 16 0.38 38.22 611.50
Nitrogen 28 19.28 1921.37 53798.28Carbon dioxide 44 21.18 2110.00 92840.21
Carbon monoxide 28 0.33 32.61 913.03
Hydrogen 2 58.83 5862.00 11724.00
MDEA 119.12 0.00 0.00 0.00
Water 18 0.00 0 0.00
Total 100.00 9964.2 159887.0
Total Mass in 1297601.56 kg/hr
Mol. Wt
Stream 12 (Feed Gas)
Mol. Wt
Stream 11 (LTS outlet)
Components
Components
11
1414
11
12
14
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Total Mass out 1297601.56 kg/hr Vap pressure of Wa
Vap pressure of Wa
Circulation rate of MDEA solution 1104.577235 m3 /hr
Partial pressure at
Total pressure bar g
H2O condensed
16.87
9.81
Formations A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225
Propane 44 -104680 1.213 0.028785
Butane 58 -125790 1.935 0.036915Nitrogen 28 0 3.28 0.000593
Carbon dioxide 44 -393509 5.457 0.001045
Carbon monoxide 28 -110525 3.376 0.000557
Hydrogen 2 0 3.249 0.000422
Oxygen 32 0 3.639 0.000506Steam 18 -241818 3.47 0.00145
Mol%
(kgmol/hr)
accomodated
Methane 16 0.38% 38.22 0.38%
Ethane 30 0.00% 0.00 0.00%
Propane 44 0.00% 0.00 0.00%
Butane 58 0.00% 0.00 0.00%
Nitrogen 28 19.28% 1921.37 19.28%
Carbon dioxide 44 21.18% 2110.00 21.18%
Carbon monoxide 28 0.33% 32.61 0.33%
Hydrogen 2 58.83% 5862.00 58.83%
Oxygen 32 0.00% 0.00 0.00%Steam 18 0.00% 0.00 0.00%
100.00% 9964.20
KJ/Kmol Gjoules/hr
Del H specific 489.8471763 KwattDel H kjoules/hr 4880933.833 4.880933833 1355.81
Heat of Formation Summation 0
Heat Supply required 0
BTU/lb Kj/kg Kj/hr Kwatt
Heat of Absorption 577 1339.217
Components Mol. Wt
Components Mol. WtHeat of Formations & Cp coef
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Heat of Absorption 124333185.2 34536.99588
Enthalpy of Lean 55759390.19 15488.7195
K
Temp of Rich solution o 298.0108983
Heat Exchanger
Flow rate T in
K
Lean MDEA sol. From Stripper 1137714.6 389.0
Rich MDEA sol. From Absorber 1230554.8 298.0
Cooler
Lean MDEA sol. From Stripper 1137714.6 353.0
Water 4303529.0 303.0
Heat of
Formations A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225
Propane 44 -104680 1.213 0.028785
Butane 58 -125790 1.935 0.036915
Nitrogen 28 0 3.28 0.000593
Carbon dioxide 44 -393509 5.457 0.001045Carbon monoxide 28 -110525 3.376 0.000557
Hydrogen 2 0 3.249 0.000422
Oxygen 32 0 3.639 0.000506
Steam 18 -241818 3.47 0.00145
Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodated
Methane 16 - 38.22 0.27%
Ethane 30 - 0.00 0.00%
Propane 44 - 0.00 0.00%
Butane 58 - 0.00 0.00%
Nitrogen 28 - 1921.37 13.57%
Carbon dioxide 44 - 2110.00 14.90%
Carbon monoxide 28 - 32.61 0.23%
Hydrogen 2 - 5862.00 41.41%
Oxygen 32 - 0.00 0.00%
Components Mol. Wt
Heat of Formations & Cp coef
Components Mol. Wt
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Steam 18 - 4192.76 29.62%
0.00% 14156.96 100.00%
KJ/Kmol Gjoules/hr
Del H specific -3523.913277Del H -49887904.29 -49.8879043
Heat of Formation Summation 0 rxn heat
Latent Heat of Condensation Sat. steam 2801.9425
sat. water 959.86
-1842.0825
Boiler Feed Water Gjoules/hr
Total heat Surplus -255.5087114
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Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)
0.38 38.22 611.50 0.00 0.00 0.00
19.28 1921.37 53798.28 0.00 0.00 0.00
21.18 2110.00 92840.21 0.00 0.00 0.00
0.33 32.61 913.03 0.00 0.00 0.0058.83 5862.00 11724.00 0.00 0.00 0.00
0.00 0.00 0.00 100.00 4192.76 75469.75693
100 9964.20 159887.01 100 4192.76 75469.76
235356.77
Treated Gas
Rich Solvent
MDEA M.wt 119.7
H20 18
CO2 44
Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)
0.00 0.00 0.00 0.49 38.22 611.50
0.00 0.00 0.00 24.46 1921.37 53798.280.00 468.89 20631.16 0.00 0.00 0.00
0.00 0.00 0.00 0.42 32.61 913.03
0.00 0.00 0.00 74.64 5862.00 11724.00
0.00 4688.90 558541.70 0.00 0.00 0.00
0.00 31030.09 558541.70 0.00 0 0
36187.88 1137714.55 100 7854.19 67046.80
kpa Mol Fract. Of water in MDEA solution
Stream 13 (Condensed Water)
Stream 14 (Lean Solvent) Stream 15 (Treated Gas)
Stream 12
Cooler
Condenser
13
12
CO2 Removal
16
15
StripperCO2 Removal
16
15
Stripper
Cooler
Condenser
1
3
12
CO2 Removal
16
15
Stripper
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ter at 314 K 7.777 0.868728121
ter at 311 K 6.624
op of Abs. 5.754455076
4601.3
7.06 127.0079625
Avg. Cp of Rich & lean solution
C D 3.77
-2.164E-06 0
-5.561E-06 0
-8.824E-06 0
-1.1402E-05 00 4000
0 -115700
0 -3100
0 8300
0 -22700
0 12100
T initial T final Tau Cp H 0 f
298 314.00 1.053691275 35.56821927 0.136424948 -285.83
298 314.00 1.053691275 53.98298133 0 0.00
298 314.00 1.053691275 76.44538172 0 0.00
298 314.00 1.053691275 101.1240889 0 0.00
298 314.00 1.053691275 29.17315617 5.625374731 0.00
298 314.00 1.053691275 36.61442408 7.753420272 -83328.93
298 314.00 1.053691275 29.17930816 0.095490169 -361.70
298 314.00 1.053691275 28.90457273 17.0047384 0.00
298 314.00 1.053691275 29.30262954 0 0.00
298 314.00 1.053691275 33.73214972 0 0.00
30.61544852 -83976.45
315.5555556 60025
Stream Sour Gas
ficients
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T out Heat Transfer Radiation loss
K Kj/hr
353.0 154410619.0 2.0%
330.6 151322406.6
311.0 180145722.2 0.0%
313.0 180145722.2
C D
-2.164E-06 0
-5.561E-06 0
-8.824E-06 0
-1.1402E-05 0
0 4000
0 -1157000 -3100
0 8300
0 -22700
0 12100
T initial T final Tau Cp H 0 f
563.00 458.60 0.814564831 48.00491689 0.129595421 -201.18
563 458.60 0.814564831 78.94244115 0 0.00
563 458.60 0.814564831 113.1205742 0 0.00
563 458.60 0.814564831 148.0378723 0 0.00
563 458.60 0.814564831 29.87373033 4.054429569 0.00
563 458.60 0.814564831 47.3353733 7.055035241 -58650.00
563 458.60 0.814564831 30.36729276 0.069945859 -254.58
563 458.60 0.814564831 28.98166792 12.00049167 0.00
563 458.60 0.814564831 31.91851899 0 0.00
ficients
OOLER SEPERATOR WATER LET DOWN
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563 458.60 0.814564831 35.26595326 10.44446083 -71617.48
33.75395859 -130723.23
200 392
290
0 J/mol
Heat of Condensation -33157.485 -1.39022E+11
-139.0215185
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CO2 Out
Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)
0.00% 0.00 0.00
0.00% 0.00 0.006.73% 2578.89 113471.37 2110.00 92840.20825
0.00% 0.00 0.00
0.00% 0.00 0.00
12.24% 4688.90 558541.70
81.02% 31030.09 558541.70
1.00 38297.89 1230554.76
Stream 16 (Rich Solvent)
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Mol%
(kgmol/hr)
accomodate T initial T final Tau Cp
0.49% 38.22 0.49% 298.00 311.00 1.043624161 35.47157627
0.00% 0.00 0.00% 298.00 311.00 1.043624161 53.78590048
0.00% 0.00 0.00% 298.00 311.00 1.043624161 76.15411779
0.00% 0.00 0.00% 298.00 311.00 1.043624161 100.7512189
24.46% 1921.37 24.46% 298.00 311.00 1.043624161 29.16199085
0.00% 0.00 0.00% 298.00 311.00 1.043624161 36.71043942
0.42% 32.61 0.42% 298.00 311.00 1.043624161 29.17528357
74.64% 5862.00 74.64% 298.00 311.00 1.043624161 28.8914872
0.00% 0.00 0.00% 298.00 311.00 1.043624161 29.31771402
0.00% 0.00 0.00% 298.00 311.00 1.043624161 33.70266249
100.00% 7854.19 100.00%
KJ/Kmol Gjoules/hr 329.88 Temp C
Del H specifi 376.8811455 kwattDel H 2960097.032 2.960097032 822.2491754
Heat of Formation Summatio 0 0
Steam Requirment in Reboiler
Cp Flow rate T oprational T ref
kg/hr K K
Stream Treated gas
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Rich Sol. Entering from Abs. 3.77 1230554.8 330.6 298.0
Lean solution leaving 3.77 1137714.6 389.0 298.0
CO2 gas leaving Stripper 0.878863636 92840.21 367.8 298
Enthalpy of Desorption - - - -
Steam Enthalpy required kj/kg 2133 174401.6235
Latent heat 4 bar abs. -
Steam required
174.4016235 TPH
psi Deg C K
System press 164.4 temp 185.6 458.6
8498.056974
Vapor pressure A B C Vap. Pressure
8.14019 1810.94 244.485 8502.251881 164
Mol%
Mole Flow
(kgmol/hr)
Mol%
accomodate
d T initial T final Tau Cp
- 38.22 0.27% 458.60 315.22 0.687357659 40.63784599
- 0.00 0.00% 458.6 315.22 0.687357659 64.2452437
- 0.00 0.00% 458.6 315.22 0.687357659 91.57177042
- 0.00 0.00% 458.6 315.22 0.687357659 120.4815756
- 1921.37 13.57% 458.6 315.22 0.687357659 29.28615871
- 2110.00 14.90% 458.6 315.22 0.687357659 45.58720927
- 32.61 0.23% 458.6 315.22 0.687357659 29.77557609
- 5862.00 41.41% 458.6 315.22 0.687357659 28.59519593
- 0.00 0.00% 458.6 315.22 0.687357659 31.26552737
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- 4192.76 29.62% 458.6 315.22 0.687357659 33.84269306
0.00% 14156.96
KJ/Kmol Gjoules/hr 42.22 Temp C
Del H specifi -4704.3491Del H -66599288.6 -66.5992886
Heat of Formation Summatio -1850.64378 0
32
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H 0 f
0.172604827 -362.61
0 0.00
0 0.00
0 0.00
7.133883057 0.00
0 0.00
0.121126601 -458.87
21.56324286 0.00
0 0.00
0 0.00
28.99085734 -821.48
Enthalpy
Kj/hr Kwatt 2% radiation loss
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151372965.9 42048.04608 98%
390315731.4 108421.0365
5695253.0 1582.014732
124333185.2 34536.99588
371998663 103332.9619
K
1.000493631
H 0 f
0.10970707 -201.18
0 0.00
0 0.00
0 0.00
3.974685 0.00
6.794482552 -58650.00
0.068582941 -254.58
11.84046452 0.00
0 0.00
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10.02294421 -71617.48
32.81086629 -130723.23
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Methanator
Temperature 400 C
Pressure 460 psig
Pressure Drop 10 psig
From CO2 Removal Unit
Reactions in Methanator
Reaction 1 CO+3H2 = CH4 +H2O 100%
Mol%
Mole Flow
(mol/hr)
Mass Flow
(kg/hr)Methane 16 0.49 38.22 611.50
Nitrogen 28 24.46 1921.37 53798.28
Carbon monoxide 28 0.42 32.61 913.03
Hydrogen 2 74.64 5862.00 11724.00
Steam 18 0.00 0.00 0.00Total 100 7854.2 67046.8
CO Consume
Reaction 1 32.61 kgmol/hr
H2 Consume
Reaction 1 97.82 kgmol/hr CH4 Produced
Reaction 1 32.61 kgmol/hr
Steam Produced
Reaction 1 32.61 kgmol/hr
Heat of Formations A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225
Propane 44 -104680 1.213 0.028785
Butane 58 -125790 1.935 0.036915
Nitrogen 28 0 3.28 0.000593
Carbon dioxide 44 -393509 5.457 0.001045
Carbon monoxide 28 -110525 3.376 0.000557
Hydrogen 2 0 3.249 0.000422
Components Mol. WtHeat of Formations & Cp coeffici
Components Mol. Wt
Stream 15 (CO2 Removal outlet)
15
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Oxygen 32 0 3.639 0.000506Steam 18 -241818 3.47 0.00145
Mol%
(kgmol/hr)
accomodate
Methane 16 0.49% 38.22 0.49%
Ethane 30 0.00% 0.00 0.00%Propane 44 0.00% 0.00 0.00%
Butane 58 0.00% 0.00 0.00%
Nitrogen 28 24.46% 1921.37 24.46%
Carbon dioxide 44 0.00% 0.00 0.00%
Carbon monoxide 28 0.42% 32.61 0.42%
Hydrogen 2 74.64% 5862.00 74.64%
Oxygen 32 0.00% 0.00 0.00%Steam 18 0.00% 0.00 0.00%
100.00% 7854.19
KJ/Kmol Gjoules/hr
Del H specific -8412.4524Del H -66073020 -66.07302011
Heat of Formation Summation -6.452059187 rxn heat
Heat Supply required -0.209185006
Heat of Formations A B
Methane 16 -74520 1.702 0.009081
Ethane 30 -83820 1.131 0.019225
Propane 44 -104680 1.213 0.028785Butane 58 -125790 1.935 0.036915
Nitrogen 28 0 3.28 0.000593
Carbon dioxide 44 -393509 5.457 0.001045
Carbon monoxide 28 -110525 3.376 0.000557
Hydrogen 2 0 3.249 0.000422
Oxygen 32 0 3.639 0.000506
Steam 18 -241818 3.47 0.00145
Mol%
Mole Flow
(kgmol/hr)
Mol%accomodate
d
Methane 16 0.91% 70.83 0.91%
Ethane 30 0.00% 0.00 0.00%
Propane 44 0.00% 0.00 0.00%
Butane 58 0.00% 0.00 0.00%
Nitrogen 28 24.67% 1921.37 24.67%
Carbon dioxide 44 0.00% 0.00 0.00%
Components Mol. Wt
Components Mol. WtHeat of Formations & Cp coeffici
Components Mol. Wt
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Carbon monoxide 28 0.00% 0.00 0.00%
Hydrogen 2 74.00% 5764.17 74.00%
Oxygen 32 0.00% 0.00 0.00%
Steam 18 0.42% 32.61 0.42%
100.00% 7788.98
KJ/Kmol Gjoules/hr Del H specific -8923.3681Del H -69503901 -69.50390139
Heat of Formation Summation -13.1632376 rxn heat
Latent Heat of Condensation Sat. steam 2801.9425
sat. water 959.86
-1842.0825
Boiler Feed Water Gjoules/hr
Total heat Surplus -66.687284
Enthalpy of condensation
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Knock out water
based on CO
Mol%
Mole Flow
(mol/hr)
Mass Flow
(kg/hr) Mol%
Mole Flow
(mol/hr)
Mass Flow
(kg/hr) Mol%0.91 70.83 1133.23 0.91 70.83 1133.23 0.00
24.67 1921.37 53798.28 24.77 1921.37 53798.28 0.00
0.00 0.00 0.00 0.00 0.00 0.00 0.00
74.00 5764.17 11528.35 74.32 5764.17 11528.35 0.00
0.42 32.61 586.95 0.00 0.00 0 100.00
100 7788.98 67046.80 100.00 7756.37 66459.85 100
C D
-2.164E-06 0
-5.561E-06 0
-8.824E-06 0
-1.1402E-05 0
0 4000
0 -115700
0 -3100
0 8300
ents
StreamStream 17 (Methanator outlet) Stream 18
MethanatorCooler and
Separator
17 18
19
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0 -22700
0 12100
T initial T final Tau Cp H 0 f Mol%
588.5555556 298.00 0.506324335 43.95583296 0.213889252 -362.61 0.91%
588.5555556 298.00 0.506324335 70.8451132 0 0.00 0.00%588.5555556 298.00 0.506324335 101.2379035 0 0.00 0.00%
588.5555556 298.00 0.506324335 132.8406393 0 0.00 0.00%
588.5555556 298.00 0.506324335 29.50397879 7.217543394 0.00 24.67%
588.5555556 298.00 0.506324335 47.81471433 0 0.00 0.00%
588.5555556 298.00 0.506324335 30.08316558 0.124895842 -458.87 0.00%
588.5555556 298.00 0.506324335 28.66829498 21.39666271 0.00 74.00%
588.5555556 298.00 0.506324335 31.84360354 0 0.00 0.00%
588.5555556 298.00 0.506324335 34.34047126 0 0.00 0.42%
28.9529912 -821.48 100.00%
315.5555556 600
315.5555556
Del H specifDel H
-6.71117841 Heat of Forma
C D
-2.164E-06 0 System press
-5.561E-06 0
-8.824E-06 0 Vapor pressu-1.1402E-05 0
0 4000
0 -115700
0 -3100
0 8300
0 -22700
0 12100
T initial T final Tau Cp H 0 f Mol%
605.00 298.00 0.492561983 44.4295088 0.40400612 -677.62 0.91%
605 298.00 0.492561983 71.78131826 0 0.00 0.00%
605 298.00 0.492561983 102.6058244 0 0.00 0.00%
605 298.00 0.492561983 134.5890846 0 0.00 0.00%
605 298.00 0.492561983 29.540659 7.287023311 0.00 24.67%
605 298.00 0.492561983 47.99771414 0 0.00 0.00%
ents
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605 298.00 0.492561983 30.12423103 0 0.00 0.00%
605 298.00 0.492561983 28.68913941 21.23118557 0.00 74.00%
605 298.00 0.492561983 31.90008202 0 0.00 0.00%
605 298.00 0.492561983 34.42792515 0.144130688 -1012.36 0.42%
29.06634569 -1689.98 100.00%
200 392
332 Del H specifDel H
0 Heat of Forma
J/mol
Heat of Condensation -33157.485 -1081203800
-1.0812038
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Mole Flow
(mol/hr)
Mass Flow
(kg/hr)0.00 0.00
0.00 0.00
0.00 0.00
0.00 0.00
32.61 586.95
32.61 586.95
Input 67046.8
Out put 67046.80
19 (Knock out Water)
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(kgmol/hr)
accomodate T initial T final Tau Cp
70.83 0.91% 298.00 605.00 2.030201342 44.4295088
0.00 0.00% 298.00 605.00 2.030201342 71.781318260.00 0.00% 298.00 605.00 2.030201342 102.6058244
0.00 0.00% 298.00 605.00 2.030201342 134.5890846
1921.37 24.67% 298.00 605.00 2.030201342 30.2561915
0.00 0.00% 298.00 605.00 2.030201342 27.30093637
0.00 0.00% 298.00 605.00 2.030201342 29.56969334
5764.17 74.00% 298.00 605.00 2.030201342 30.17386936
0.00 0.00% 298.00 605.00 2.030201342 27.83943504
32.61 0.42% 298.00 605.00 2.030201342 36.59241098
7788.98 100.00%
KJ/Kmol Gjoules/hr 332.00 Temp C
9317.657708
72575013.52 72.57501352
tion Summatio -13.1632376 -0.20918501
psi Deg C
192.5765668 temp 25 298
9956.339507
e A B C Vap. Pressure8.14019 1810.94 244.485 26.31400976 0.508968347
Mole Flow
(kgmol/hr)
Mol%accomodate
d T initial T final Tau Cp
70.83 0.91% 298.00 315.22 1.057792692 35.60756139
0.00 0.00% 298 315.22 1.057792692 54.063194
0.00 0.00% 298 315.22 1.057792692 76.56391861
0.00 0.00% 298 315.22 1.057792692 101.2758359
1921.37 24.67% 298 315.22 1.057792692 29.177705
0.00 0.00% 298 315.22 1.057792692 36.57530672
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0.00 0.00% 298 315.22 1.057792692 29.18094781
5764.17 74.00% 298 315.22 1.057792692 28.90990388
0.00 0.00% 298 315.22 1.057792692 29.29648401
32.61 0.42% 298 315.22 1.057792692 33.74416304
7788.98
KJ/Kmol Gjoules/hr 42.22 Temp C500.4279353
3897821.245 3.897821245
tion Summatio -13.1632376 0
629.6
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H 0 f
0.40400612 -677.62
0 0.000 0.00
0 0.00
7.46352926 0.00
0 0.00
0 0.00
22.329949 0.00
0 0.00
0.153192193 -1012.36
30.35067657 -1689.98
K0.00264294
H 0 f
0.323786445 -677.62
0 0.00
0 0.00
0 0.00
7.197490635 0.00
0 0.00
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0 0.00
21.39456069 0.00
0 0.00
0.141268154 -1012.36
29.05710592 -1689.98
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Ammonia Conversion Loop
Temperature 400 C
Pressure 2000 psig
Pressure Drop 10 psig
From Methanator
Reactions in Ammonia Converter
Reaction 1 N2+3H2 = 2NH3 25% based onN2
Iteration No. 1
Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%Methane 16 0.91% 70.83 1133.23 16.66%
Nitrogen 28 24.77% 1921.37 53798.28 16.61%
Hydrogen 2 74.32% 5764.17 11528.35 49.82%
Ammonia 17 0.00% 0.00 0.00 16.91%
Total 100.00% 7756.4 66459.9 100.00%
H2 Consume Calculations for Purge stream 20 Rate
Reaction 1 5552.32 kgmol/hr Feed Stream Flow 7756.4
N2 Consume 5552.39 Feed Stream Inert 0.01
Reaction 1 1850.77 kgmol/hr Required Inert Conc. 15%
1850.77
NH3 Produced Purge Stream 20 flow 378.65
Reaction 1 3701.55 kgmol/hr Recycle Stream 21 Flow 29380.98
66459.9
3701.55 66458.27
R /F 3.787982016
Note: This indicates that at the start-up, until the system get stabilized, recycle is required after
Scale up Factor Calculations
NH3 production based on 100 kgmol/hr ofNaphthas Feed
Scale up Factor
All the stream flow should be multiplied by this factor to get the desired
Components Mol. Wt
Stream 18 (Methanator Outlet) Strea
Ammonia
Converter18
24
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ammonia price
dollar
Total Input
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Recycle Stream Purge Stream
Liquid Ammonia
Sep. Efficiency 65% N2 :H2 3
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%5570.60 89129.64 15.00% 5570.60 89129.64 0.00%
5552.32 155464.92 19.93% 7403.09 207286.57 0.00%
16657.17 33314.33 59.80% 22209.56 44419.11 0.00%
5655.65 96145.99 5.26% 1954.10 33219.70838 100.00%
33435.80 374054.89 100.00% 37137.35 374055.03 100.00%
kgmol/hr Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr) Mol%
mol% Methane 18.72% 70.83 1133.23 18.72%
mol% Nitrogen 18.66% 70.65 1978.09 18.66%
Hydrogen 55.97% 211.94 423.88 55.97%
NH3 6.65% 25.19 428.18 6.65%
kgmol/hr
kgmol/hr 100.00% 378.65 3963.37 100.00%
66459.85 66458.27 1.59
7756.4 4054.82that all the stream should be purged.
62494.89 kg/hr 62.49489181 TPH
1499.9 Tonnes/day
1.0
roduction rate.
20 (Converter outlet) Stream (25) (Mixed feed)
Purge Stream 23 Re
Stream
Cooler and
Ammonia
Separator
20 21
22
23
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Put Basis
Required 1.981525046 2265.2595
4743.387682
31538.7847 31.5387847 756.9308328
Nh3/ton naphtha 1.981525046
792.6100185 504.6618017
287.9482168 145.3164659
0.504661802
-
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Mole Flow
(kgmol/hr) Mass Flow (kg/hr) Mol%
Mole Flow
(kgmol/hr)
Mass Flow
(kg/hr)0.00 0.00 18.72% 5570.60 89129.64
0.00 0.00 18.66% 5552.32 155464.92
0.00 0.00 55.97% 16657.17 33314.33
3676.17 62494.89 6.65% 1979.48 33651.10
3676.17 62494.89 100.00% 29759.56 311560.00 -0.14
Mole Flow
(kgmol/hr) Mass Flow (kg/hr)
5499.78 87996.41
5481.67 153486.84
16445.23 32890.45
1954.29 33222.91
29380.96 311560.00
29380.98 307596.62
1133.23
1.447523411
Stream 21 (after seperatorLiquid Ammonia)
ycle Stream 24
2 (Liquid Ammonia)
-
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Over All composition
Carbon 26169.9768 - -
H2 5108.211 - -
Methane 16 - - 20383.22
Ethane 30 - - -
Propane 44 - - -
Butane 58 - - -
Nitrogen 28 - - -
Carbon dioxide 44 - - 560.54
Carbon monoxid 28 - - 25035.94
Hydrogen 2 306.3978 - 2158.04
Oxygen 32 - - -
Steam/Water 18 - 137392.3782 120839.2201
Argon 40 - - -
MDEA sol. - - -
Ammonia - - -
Total 31584.5856 137392.3782 168976.9638
0
Total Input 235356.8
Total output 235356.8
Input output
St 1 31584.5856 co2 out 92840.20825
St 5 -3762.258051 st 13 75469.75693
St 2 137392.3782 st 19 586.9464585
N.gas input 0 st 23 3963.374505
Pre- Reformer
Components Mol. Wt Stream 1 (Pre-R1) Stream 2 (Pre-R2) Stream 3 (Pre-R3)
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St 7 70142.06014 st 22 62494.89181
235356.7659 1.587933805
235356.7659 235356.7659
235.3567659
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- -
- -
20383.21625 - 5095.80 -
0 - 0.00 -
0 - 0.00 -
0 - 0.00 -
0 - 0.00 53798.27914
560.538447 - 33113.57 -
25035.94447 - 31073.35 -
2158.044525 - 9370.51 -
- - - 16343.781
120839.2201 -3762.258051 86561.47 -
- -
- -
- -
168976.9638 -3762.258051 165214.7057 70142.06014
0
kg/hr
kg/hr
Stream 5 (P-R5) Stream 6 (P-R6) Stream 7 (S-R7)
Reformer Primary & Secondary
Stream 4 (P-R4)
-
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0.000674692
-
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611.50 611.50 611.50 611.50
- -
- -
- -
53798.28 53798.28 53798.28 53798.28
58406.02 58406.02 87101.18 92840.21
22825.70 22825.70 4565.14 913.03
10158.81 10158.81 11463.13 11724.00
0.00 0.00
89556.47 89556.47 77817.54 75469.75693
235356.7659 235356.7659 235356.7659 235356.7659
0
Stream 11 (S-C11)
Shift Convertors
Stream 8 (S-R8) Stream 9 (S-C9) Stream 10 (S-C10)
-
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-
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611.50 611.50
-
-
-
53798.28 53798.28
92840.21 20631.16
913.03 913.03
11724.00 11724.00
75469.75693 558541.70
558541.70
159887.009 75469.75693 1137714.552 67046.80071
0 1297601.561
Stream 12 (C-S12) Stream 13 (C-S13)
Water Seperator
Stream 14 (C-S14) Stream 15 (C-A15)
CO2 Absorption Strippin
-
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-
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1133.23 1133.23
53798.28 53798.28
113471.37
11528.35 11528.35
558541.70 586.95 586.95
558541.70
1230554.76 67046.80071 66459.85425 586.9464585
1297601.561 0.00
0
Input
Stream 16 (C-A16)
g
Stream 17 (M-R17) Stream 18 (M-R18) Stream 19 (M-R18)
Methanator
-
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-
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89129.64 89129.64 1133.23
155464.92 155464.92 1978.09
33314.33 33314.33 423.88
96145.99 33651.10 62494.89 428.18
374054.8868 311559.995 62494.89181 3963.374505
Stream 20 (S-L20) Stream 21 (S-L21)
Stream 22 (S-L22) Stream 23 (S-L23)
-
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-
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174/178
-
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175/178
-
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176/178
235355.2
-
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177/178
-
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178/178