Heater (HE-02)

Neraca Massa Heater CO2

Intlet
Komponen
Kg/Jam Kmol/Jam
CO2 129916.38 2950.97
H2 17705.81 8852.90
CH3OH 0.00 0.00
H2O 0.00 0.00
CH4 57.24 3.57
Total 147679.42 11807.44

Neraca Energi Heater CO2

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 * (
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 27.437 4.23E-02
H2 2 25.399 2.02E-02
CH3OH 32.042 40.046 -3.83E-02
H2O 18.015 33.933 -0.00842
CH4 16.043 34.942 -4.00E-02

CP FASE CAIR
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 * (
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 -338.956 5.28E+00
H2 2 50.607 -6.11E+00
 CH3OH 32.042 40.152 3.10E-01
H2O 18.105 92.053 -4.00E-02

ENTHALPY PENGUA
Hvap= A( 1- T/TC)^n

Komponen BM A Tc
CO2 44.025 15.326 304.19
H2 2 0.659 33.18
CH3OH 32.042 52.723 512.58
H2O 18.015 52.053 647.13

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2

Komponen BM A B
CO2 44.025 35.0169 -1.51E+03
H2 2 3.4132 -4.13E+01
CH3OH 32.042 45.6171 -3.24E+03
H2O 18.015 29.8605 -3.15E+03

HEATER

INPUT
TEMPERATUR T (Reff)
P (bar) o
C K o
C
21 55.85 329 25

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi

CO2 44.025 129916.376623579 2950.968237 1
Total 2950.968237

OUTPUT
TEMPERATUR T (Reff)
P (bar) o
C K o
C
21 162.68 435.83 25

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi

CO2 44.025 129916.376623579 2950.968237 1
Total 2950.968237

KEBUTUHAN PANAS
 Q 7372520.018 kj/jam
Panas Laten 2645.6 kj/kg
Kebutuhan Steam 2786.710 kg/jam

Panas Laten 100 C

Superheated Steam 300 C
200 C
Elementary Principles. Felder

laju alir BM laju alir

Komponen
masuk (kg/jam) (kg/kmol) masuk (kmol/jam)
CO2 129916.38 44.025 2950.97
eater (HE-02)

Komponen BM
CO2 44.025
H2 2
CH3OH 32.042 Heater
H2O 18.015
CH4 16.043

CP FASE GAS
(sumber : yaws)

3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D E
-1.96E-05 4.00E-09 -2.99E-13
-3.85E-05 3.19E-08 -8.76E-12
2.45E-04 -2.17E-07 5.99E-11
0.0000299 -1.78E-08 3.69E-12
1.92E-04 -1.53E-07 3.93E-11

CP FASE CAIR
(sumber : yaws)

3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D
-2.33E-02 3.60E-05
3.09E-01 -4.15E-03
 -1.03E-03 1.46E-06
-2.11E-04 5.35E-07

ENTHALPY PENGUAPAN
(sumber : yaws)

n
0.227
0.38
0.377
0.321

TEKANAN UAP MURNI

(sumber : yaws)

C D E
-1.13E+01 9.34E-03 1.71E-09
1.09E+00 -6.69E-10 1.46E-04
-1.40E+01 6.64E-03 -1.05E-13
-7.30E+00 2.42E-09 1.81E-06

HEATER

T (Reff)
K
298.15

A B C D E
27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13

T (Reff)
K
298.15

A B C D E
27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13

aliran panas masuk aliran panas keluar

 Hin 9082315.105 Hout 16454835.123
Q heater 7372520.018
Total 16454835.123 16454835.123

Aliran Panas Masuk Aliran Panas Keluar

Komponen
Kj/Jam Kj/Jam
CO2 9082315.11 16454835.1233714
Steam 7372520.02
Total 16454835.1233714 16454835.12
Cpg dT (J/mol) H sensibel (kJ/jam)
3077.74071979 9082315.10511104
3077.74071979 9082315.10511104

Cpg dT (J/mol) H sensibel (kJ/jam)

5576.08005344 16454835.1233714
5576.08005344 16454835.1233714
 Heater (HE-01)

Neraca Massa Heater H2

Intlet Komponen
Komponen
Kg/Jam Kmol/Jam CO2
CO2 129916.38 2950.97 H2
H2 17705.81 8852.90 CH3OH
CH3OH 0.00 0.00 H2O
H2O 0.00 0.00 CH4
CH4 10.74 0.67 N2
N2 36.47 1.30
Total 147669.40 11805.84

Neraca Energi Heater H2

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4 (sumber : yaws)
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 * (
T reff = 25 C 298.15 K

Komponen BM A B C
CO2 44.025 27.437 4.23E-02 -1.96E-05
H2 2 25.399 2.02E-02 -3.85E-05
CH3OH 32.042 40.046 -3.83E-02 2.45E-04
H2O 18.015 33.933 -0.00842 0.0000299
CH4 16.043 34.942 -4.00E-02 1.92E-04

CP FASE CAIR
Cp = A + BT +CT^2 +DT ^3 +ET^4 (sumber : yaws)
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 * (
T reff = 25 C 298.15 K

Komponen BM A B C
CO2 44.025 -338.956 5.28E+00 -2.33E-02
 H2 2 50.607 -6.11E+00 3.09E-01
CH3OH 32.042 40.152 3.10E-01 -1.03E-03
H2O 18.015 92.053 -4.00E-02 -2.11E-04

ENTHALPY PENGUAPAN
Hvap= A( 1- T/TC)^n (sumber : yaws)

Komponen BM A Tc n
CO2 44.025 15.326 304.19 0.227
H2 2 0.659 33.18 0.38
CH3OH 32.042 52.723 512.58 0.377
H2O 18.015 52.053 647.13 0.321

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2 (sumber : yaws)

Komponen BM A B C
CO2 44.025 35.0169 -1.51E+03 -1.13E+01
H2 2 3.4132 -4.13E+01 1.09E+00
CH3OH 32.042 45.6171 -3.24E+03 -1.40E+01
H2O 18.015 29.8605 -3.15E+03 -7.30E+00

HEATER

INPUT
TEMPERATUR T (Reff)
P (bar)
C
o
K o
C K
21 5 278.15 25 298.15

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi A

H2 2 17705.81 8852.90471 0.9997773485 25.399
CH4 16.043 10.74 0.669513183 7.5609547048E-05 34.942
N2 28.013 36.47 1.302038339 0.000147042 29.342
Total 8854.876262 1

OUTPUT
TEMPERATUR T (Reff)
P (bar)
C
o
K o
C K
21 162.68 435.83 25 298.15

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi A

H2 2 17705.80942059 8852.90471 0.9997773485 25.399
CH4 16.043 10.74 0.669513183 7.5609547048E-05 34.942
 N2 28.013 36.47 1.302038339 0.000147042 29.342
Total 8854.876262 1

KEBUTUHAN PANAS aliran panas masuk

Q 40456581.232 kj/jam Hin
Panas Latent 2645.6 kj/kg Q heater
Kebutuhan Steam 15292.025 kg/jam Total

Panas Laten 100 C

Komponen
Superheated Steam 300 C
200 C H2
Elementary Principles. Felder CH4
N2
Steam
laju alir BM laju alir Total
Komponen
masuk (kg/jam) (kg/kmol) masuk (kmol/jam)
H2 17705.81 2 8852.90
E-01)

BM
44.025
2 Heater
32.042
18.015
16.043
28.013

* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5) 308.15 298.15

287.8737959245 28.764042

D E
4.00E-09 -2.99E-13
3.19E-08 -8.76E-12
-2.17E-07 5.99E-11
-1.78E-08 3.69E-12
-1.53E-07 3.93E-11

AIR

* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

D
3.60E-05
 -4.15E-03
1.46E-06
5.35E-07

ALPY PENGUAPAN

P MURNI

D E
9.34E-03 1.71E-09
-6.69E-10 1.46E-04
6.64E-03 -1.05E-13
2.42E-09 1.81E-06

HEATER

B C D E Cpg dT (J/mol)
2.02E-02 -3.85E-05 3.19E-08 -8.76E-12 -574.28786969
-4.00E-02 1.92E-04 -1.53E-07 3.93E-11 -719.38779992
-3.54E-03 1.01E-05 -4.31E-09 2.59E-13 -581.15111114
-1874.8267808

B C D E Cpg dT (J/mol)
2.02E-02 -3.85E-05 3.19E-08 -8.76E-12 3994.43642996
-4.00E-02 1.92E-04 -1.53E-07 3.93E-11 5418.0165706
 -3.54E-03 1.01E-05 -4.31E-09 2.59E-13 4020.31620277
13432.7692033

aliran panas masuk aliran panas keluar

-5085354.11 Hout 35371227.125128
40456581.23
35371227.13 35371227.125128

Aliran Panas Masuk Aliran Panas Keluar

Kj/Jam Kj/Jam
-5084115.79 35362365.0857743
-481.64 3627.4335214651
-756.68 5234.6058322841
40456581.23
35371227.13 35371227.13
H sensibel (kJ/jam)
-5084115.7866081
-481.6396159677
-756.6810276588
-5085354.1072517

H sensibel (kJ/jam)
35362365.0857743
3627.4335214651
5234.6058322841
35371227.125128
 Neraca Energi

Input
P 21 bar
T 435.83 K Tref 298.15

Komponen BM A B C D E
CO2 44.025 27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13
H2 2 25.399 2.02E-02 -3.85E-05 3.19E-08 -8.76E-12
CH4 16.043 34.942 -4.00E-02 1.92E-04 ### 3.93E-11
N2 28.013 29.342 -3.54E-03 1.01E-05 ### 2.59E-13

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi A B

CO2 44.025 129916.38 2950.96824 0.24995825 27.437 4.23E-02
H2 2 17705.81 8852.90471 0.74987475 25.399 2.02E-02
CH4 16.043 10.74 0.66951318 5.671E-05 34.942 -4.00E-02
N2 28.013 36.47 1.30203834 0.00011029 29.342 -3.54E-03
Total 11805.8445 1

Output

P 50.5 bar
T 473.130918965 K Tref 298.15

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi A B

CO2 44.025 129916.38 2950.96824 0.24995825 27.437 4.23E-02
H2 2 17705.81 8852.90471 0.74987475 25.399 2.02E-02
CH4 16.043 10.74 0.66951318 5.671E-05 34.942 -4.00E-02
N2 28.013 36.47 1.30203834 0.00011029 29.342 -3.54E-03
Total 147669.40 11805.8445 1

Q 14385466.9643 kJ/Jam

Aliran Masuk Aliran Keluar

Hin 51826062.2 Hout 66211529.2
Q 14385467
Total 66211529.2 66211529.2

SPEK ALAT

Coret coretan kompresor (HITUNG MANUAL DAN HITUNG EXCEL) K

R 8.314 kJ/Kmol.K
Tin 435.83 K 162.68 C
Pin 21 bar
Pout 50.5 bar

Rumus menghitung kebutuhan tenaga kompresor

 w
z x R xT1 n
M
x
n 1

x  P2 / P1  1 
n1/ n
Coulson hal.82 pers. 3.31

menghitung nilai n menggunakan metode pitzer hal 97

z 1   BPc / RTc  x  Pr / Tr   persamaan 3.58

BPc T
 B 0  wB , persamaan 3.59 Komp. A
Rtc
CO2 27.437
Bº = 0.083 - (0.422 / Tr ^ 1.6) persamaan 3.61 H2 25.399
B΄ = 0.139 - (0.172 / Tr ^ 4.2) persamaan 3.62 CH4 34.942
w= -log (Pr) - 1 N2 29.342

menghitung volume kompresor

z x n x R xT
V
P

Tabel komponen Data Yaws 1999, critical p

Komponen BM (Kg/mol) F1 (kg/jam) ni (kmol/jam) Xi Bm.Xi Komponen
CO2 44.025 129916.38 2950.96824 0.24995825 11.00441 CO2
H2 2 17705.81 8852.90471 0.74987475 1.49975 H2
CH4 16.043 10.74 0.66951318 5.671E-05 0.00091 CH4
N2 28.013 36.47 1.30203834 0.00011029 0.003089 N2
Total 11805.8445 1 12.50816

Menghitung komponen
Komponen Tc (K) Pc (Bar) Tr= T/Tc Pr= P/Pc w Bo
CO2 304.19 73.82 1.43275584 0.28447575 -0.45405 0.0592624
H2 33.18 13.13 13.1353225 1.59939071 -1.20395 0.0823148
CH4 190.58 46.04 2.28686116 0.45612511 -0.65908 0.0717661
N2 126.1 33.94 3.45622522 0.61873895 -0.79151 0.0771984
Total

Volume total 2022602.29864 cm3 2.0226023 m3/jam 0.000562 m3/s

Kapasitas panas 132.589691058
dari fig 3.6 coulson hal 83 didapat efisiensi kompresor 67%

y = Cp/ CP-R 1.0668996481 1.06689965

m = y-1 / y x efisiensi 0.0935891405

n=1/(1-m) 1.1032524484

menghitung jumlah stage

Rc=(P2/P1)^1/n 2.2151741494

z= 3.983306142

menghitung BM campuran gas

M= axi.Bmi 12.5081607726 Kg/Kmol

Menghitung power kompresor

 w
z x R xT1 n
M
x
n 1

x  P2 / P1 
n1/ n

1

(-w)= 1055.24748071 Kj/Kg

kerja aktual kompresor = -w/efisiensi
1574.99623987 Kj/Kmol

Cek Suhu (T2)

(  1) / 
 P2 
T 2  T1 
 P 
 1 

m= 0.0935891405
T2= 473.130918965 K 200.0 C

Kebutuhan tenaga kompresor :

umpan masuk = 11805.8444986 kmol/jam 118.058445 kmol/jam
tenaga kompresor = umpan masuk x kerja kompresor
18594160.6938 Kj/Jam 185941.607 Kj/Jam
5165044.63716 watt atau J/s 51650.4464 watt atau J/s
5165.04463716 kw 51.6504464 kw
6926.32485843 Hp 69.2632486 Hp
Menghitung Pipa
Di opt= 3,9.Qf 0,45 ρ 0,13
Densitas gas
faktor keamanan= 25% P 50.5 bar
Qf= 0.7022924648 R 0.083 L.bar/K.mol
Di opt= 5.6821818652 in T 435.83 K
IPS= 3 in BM 44.025 g/mol
OD= 3.5 in ρ= BM.P/RT
Sch= 80 61.46042 g/l
ID= 2.9 in
A= 0.432 in2
 C D E Cp (J/mol) H (kJ/Jam)
### 4.00E-09 ### 5576.080053 16454835.12
### 3.19E-08 ### 3994.43643 35362365.09
1.92E-04 -1.53E-07 3.93E-11 5418.016571 3627.433521
1.01E-05 -4.31E-09 2.59E-13 4020.316203 5234.605832
19008.84926 51826062.25

C D E Cp (J/mol) H (kJ/Jam)
### 4.00E-09 ### 7179.6458 21186906.71
### 3.19E-08 ### 5084.572929 45013239.63
1.92E-04 -1.53E-07 3.93E-11 7048.928213 4719.350367
1.01E-05 -4.31E-09 2.59E-13 5117.762604 6663.523123
24430.90955 66211529.21

PEK ALAT

KOMPRESOR
 25 C 298.15 K
B C D E Cp
4.23E-02 -1.96E-05 4.00E-09 -2.99E-13 38.41847536
2.02E-02 -3.85E-05 3.19E-08 -8.76E-12 28.76404207
### 1.92E-04 ### 3.93E-11 36.33700884
### 1.01E-05 ### 2.59E-13 29.07016479

Data Yaws 1999, critical properties and acentric factor

BM Tf (K) Tb (K) Tc (K) Pc (bar) Vc (cm3/mol) Rho (gr/cm3) Zc
44.025 216.58 194.67 304.19 73.82 94 0.4682 0.2774
2 13.95 20.39 33.18 13.13 64.2 0.0314 0.305
16.043 90.67 111.66 190.58 46.04 99.3 0.1616 0.288
28.013 63.15 77.35 126.1 33.94 90.1 0.3109 0.292

B' Pr/Tr BPc/RTc z n (kmol) V (cm3) Cp

0.101016 0.198551451 0.013397 1.002659942 2950.968237 510535.61744 38.41847536
0.138997 0.121762576 -0.08503 0.989646441 8852.90471 1511728.162 28.76404207
0.13367 0.199454657 -0.01633 0.996742176 0.669513183 115.14625433 36.33700884
0.138059 0.179021595 -0.03208 0.994257583 1.302038339 223.37292496 29.07016479
3.983306142 2022602.2986 132.5896911

0.561834 dm3/s
L.bar/K.mol
Omega
0.228
-0.22
0.011
0.04
 Reaktor Fixe

Neraca Massa

Kapasitas 600,000 ton/tahun

jumlah hari kerja 330 hari
jumlah jam kerja 24 jam
Produksi 1 jam 75757.58 kg/jam

Spesifikasi produk 99.85% 0.9985

Spesifikasi produk 75643.94
2360.77

Konversi 80 % (Leonie E. Lucking, 2017)

Co2 3H2 CH3OH

m 2950.97 8852.90
r 2360.77 2360.77 2360.77
s 590.19 6492.13 2360.77

Inlet Reaksi
Komponen
Kg/Jam Kmol/Jam Kg/Jam
CO2 129916.38 2950.97 103933.10
H2 17705.81 8852.90 4721.55
CH3OH 0.00 0.00 -75643.94
H2 O 0.00 0.00 -42529.35
CH4 10.74 0.67 0.00
N2 36.47 1.30 0.00
Total 147669.40 11805.84 -9518.64
Kg/h Total 147669.40 14
11805.8444985827

Neraca Energi

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 * (T
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 27.437 4.23E-02
H2 2 25.399 2.02E-02
CH3OH 32.042 40.046 -3.83E-02
H2O 18.015 33.933 -0.00842
CH4 16.043 34.942 -4.00E-02
N2 28.013 29.342 -3.54E-03

Komponen Harga ΔH°f ( kJ/mol )

CH4 -74.870
N2
H2 O -241.83
CO2 -393.509 -393.509
H2 0
CH3OH -201.83 -443.66

Reaksi
Co2 3H2 CH3OH H2O

Penentuan Entalphi

ΔHR(298,15K) = o
f
produk - of,reaktan
(of CH3OH + H2O) – (of CO2 + 3.of H2)
-49.321 Kj/mol
produk -116435763.524389 Kj/mol
panas reaksi total -116435763.524389 Kj/mol

Temperatur o
C K
Ref 25 298.15
Input 200 473.15
Output 200 473.15

Input
 Komponen Kmol/Jam ʃCP dT H sensible
CO2 2950.968236765 7180.4756088064 21189355.4464534
H2 8852.904710295 5085.1311278977 45018181.3146334
CH3OH 0 8885.7207647026 0
H2O 0 5989.4818077885 0
CH4 0.6695131833 7049.7819799526 4719.9219751088
N2 1.3020383393 5118.3250994467 6664.2555126984
Total 11805.8444985827 66218920.9385746

Output

Komponen Kmol/Jam ʃCP dT H sensible

CO2 590.193647353 7180.4756088064 4237871.08929068
H2 6492.130120883 5085.1311278977 33013332.9640645
CH3OH 2360.774589412 8885.7207647026 20977183.7899204
H2O 2360.774589412 5989.4818077885 14139816.4555725
CH4 0.6695131833 7049.7819799526 4719.9219751088
N2 1.3020383393 5118.3250994467 6664.2555126984
Total 11805.8444985827 72379588.4763358

Aliran panas masuk Aliran panas keluar

Hsensible in 66218920.939 Hsensible out
Hreaksi 116435763.524389 Qpendingin

Total 182654684.463 Total

Aliran panas masuk Aliran panas keluar

Hsensible in 66218920.939 Hsensible out
Hreaksi -116435763.524389 Qpendingin

Total -50216842.586 Total

Note
Reaksi nya gapake di bagi minus ya shay
takutnya nanti diminta sama bapaknya gapake dibagi minus.
 dan juga reaksi kita itu kan eksotermis jadi gapake dibagi minus tuh
Reaksi nya dibagi minus ya shay
takutnya gak ditanya sma bapak dan pengen plus aja haha
and so, kita bimbingan nanti hasilnya gmn, kalo pake yg plus yaudah fix kita kelar

Note
Reaktor lampiran NE bikin 2 ya
yang satu pake minus tabelnya
yang satu pake plus tabelnya.. Paham kan shay :D
Love you shaaay semangat ngerjainnya ya biar kita cepet wisuda hahaha
 Reaktor Fixed Bed Multitube

Komponen BM
CO2 44.025
H2 2
CH3OH 32.042
H2O 18.015
CH4 16.043
N2 28.013
Kg/Jam
Kmol/jam

H2O

2360.77
2360.77

Reaksi Outlet
Kmol/Jam Kg/Jam Kmol/Jam
2360.77 25983.28 590.19
2360.77 12984.26 6492.13
-2360.77 75643.94 2360.77
-2360.77 42529.35 2360.77
0.00 10.74 0.67
0.00 36.47 1.30
0.00 157188.04 11805.84
147669.40
11805.8444985827

CP FASE GAS
(sumber : yaws)
4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D E
-1.96E-05 4.00E-09 -2.99E-13
-3.85E-05 3.19E-08 -8.76E-12
2.45E-04 -2.17E-07 5.99E-11
0.0000299 -1.78E-08 3.69E-12
1.92E-04 -1.53E-07 3.93E-11
1.01E-05 -4.31E-09 2.59E-13

-50.151
 Aliran Panas Masuk
Komponen
Kj/Jam
CO2 21189355.4464534
H2 45018181.3146334
CH3OH 0
H2O 0
CH4 4719.9219751088
N2 6664.2555126984
Hreaksi 116435763.52
Qpendingin 0
Total 182654684.46

Aliran panas keluar laju alir

Komponen
72379588.476 keluar (kg/jam)
110275095.987 CO2 25983.28
H2 12984.26
182654684.463 CH3OH 75643.94
H2 O 42529.35
Aliran panas keluar CH4 10.74
72379588.476 N2 36.47
-122596431.062

-50216842.586
gi minus tuh

g plus yaudah fix kita kelar

 F1 (H2)

Reaktor
F2 (CO2)

Inlet Reaksi
Komponen
Kg/Jam Kg/Jam
CO2 129916.38 103933.10
H2 17705.81 4721.55
CH3OH 0 -75643.94
H2O 0 -42529.35
CH4 10.741 0.00
N2 36.474 0.00
Total 147669.40 -9518.64
Kg/h Total 147669.40 147669.40
Aliran Panas Keluar
Kj/Jam
4237871.09
33013332.96
20977183.79
14139816.46
4719.92
6664.26
0
110275095.99
182654684.46

BM laju alir
(kg/kmol) keluar (kmol/jam)
44.025 590.19
2 6492.13
32.042 2360.77
18.015 2360.77
16.043 0.67
28.013 1.30
 Outlet
Kg/Jam
25983.28
12984.26
75643.94
42529.35
10.74
36.47
157188.04
147669.40
 Expansion Valve (EV-01)

Input Output
Komponen
Kg/Jam Kg/Jam
CO2 25983.28 25983.28
H2 12984.26 12984.26
CH3OH 75643.94 75643.94
H2O 42529.35 42529.35
CH4 10.74 10.74
N2 36.47 36.47
Sub Total 157188.04 157188.04
Total 157188.04 157188.04

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4)
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 27.437 4.23E-02
H2 2 25.399 2.02E-02
CH3OH 32.042 40.046 -3.83E-02
H2O 18.015 33.933 -0.00842
CH4 16.043 34.942 -4.00E-02

CP FASE CAIR
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4)
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 -338.956 5.28E+00
H2 2 50.607 -6.11E+00
 CH3OH 32.042 40.152 3.10E-01
H2O 18.015 92.053 -4.00E-02

ENTHALPY PENGUAPAN
Hvap= A( 1- T/TC)^n

Komponen BM A Tc
CO2 44.025 15.326 304.19
H2 2 0.659 33.18
CH3OH 32.042 52.723 512.58
H2O 18.015 52.053 647.13

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2

Komponen BM A B
CO2 44.025 35.0169 -1.51E+03
H2 2 3.4132 -4.13E+01
CH3OH 32.042 45.6171 -3.24E+03
H2O 18.015 29.8605 -3.15E+03

Expander Valve

INPUT
TEMPERATUR T (Reff)
P (bar) o
C K o
C
50.5 200 473.15 25

INPUT

Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi

CO2 44.025 25983.28 590.193647353 0.0499916501
H2 2 12984.26 6492.130120883 0.5499081511
CH3OH 32.042 75643.94 2360.774589412 0.1999666004
H2O 18.015 42529.35 2360.774589412 0.1999666004
CH4 16.043 10.74 0.6695131833 5.671031695E-05
N2 28.013 36.47 1.3020383393 0.0001102876
Total 157188.04 11805.8444985827 1

MENENTUKAN SUHU KELUAR VALVE

P 20 bar
Treff 25 298.15 K
Komponen Kmol Xi A B
CO2 590.193647353 0.0499916501 27.437 4.23E-02
H2 6492.130120883 0.5499081511 25.399 2.02E-02
CH3OH 2360.774589412 0.1999666004 40.046 -3.83E-02
H2O 2360.774589412 0.1999666004 33.933 -0.00842
CH4 0.6695131833 5.671032E-05 34.942 -4.00E-02
N2 1.3020383393 0.0001102876 29.342 -3.54E-03
Total 11805.8444985827 1

Cp (25 C) 211.3906684178 kJ/kmol.K

R 8.314 kJ/kmol.k
Rules of Thumb Chemical Engineer Third Edition hal 129

Rumus
k=𝐶�/𝐶𝑣=𝐶�/
(𝐶� −�)
K 1.0409402029
K-1 0.0409402029
K-1/K 0.0393300237

Rumus

Δ𝐻=𝐶� x �1 x 〖 ((1−
ΔH
(𝑃2/𝑃1) 〗1789.025119976
^((𝑘−1)/𝑘))xkJ/kmol
0,5
Rumus
�2=�1 x 〖 (𝑃2/𝑃1) 〗 ^((𝑘−1)/𝑘)
+ 〖 (Δ𝐻/𝐶�) 〗 ^
T2 464.6868775104 K
191.5368775104 C

Pout 20.0000 bar

Tout 191.5369 464.6869 K
Treff 25.0000 298.1500 K
 Komponen Kmol Xi A B
CO2 590.193647353 0.0499916501 27.437 4.23E-02
H2 6492.130120883 0.5499081511 25.399 2.02E-02
CH3OH 2360.774589412 0.1999666004 40.046 -3.83E-02
H2O 2360.774589412 0.1999666004 33.933 -0.00842
CH4 0.6695131833 5.671032E-05 34.942 -4.00E-02
N2 1.3020383393 0.0001102876 29.342 -3.54E-03
Total 11805.8444985827 1

Hitungan panas yang diperlukan expander :

dHev= dHin - dHout

dHev= 3,651,850.9469

Neraca energi total EV

Aliran Panas Masuk Aliran Panas Keluar
Hin 72379588.4763358 Hout 68,727,737.5295
Hev 3651850.94686253
TOTAL 72379588.4763358 TOTAL 72379588.4763358
on Valve (EV-01)

CP FASE GAS
(sumber : yaws)

) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D E
-1.96E-05 4.00E-09 -2.99E-13
-3.85E-05 3.19E-08 -8.76E-12
2.45E-04 -2.17E-07 5.99E-11
0.0000299 -1.78E-08 3.69E-12
1.92E-04 -1.53E-07 3.93E-11

FASE CAIR
(sumber : yaws)

) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D
-2.33E-02 3.60E-05
3.09E-01 -4.15E-03
 -1.03E-03 1.46E-06
-2.11E-04 5.35E-07

THALPY PENGUAPAN
(sumber : yaws)

n
0.227
0.38
0.377
0.321

AN UAP MURNI
(sumber : yaws)

C D E
-1.13E+01 9.34E-03 1.71E-09
1.09E+00 -6.69E-10 1.46E-04
-1.40E+01 6.64E-03 -1.05E-13
-7.30E+00 2.42E-09 1.81E-06

Expander Valve

T (Reff)
K
298.15

A B C D E
27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13
25.399 2.02E-02 -3.85E-05 3.19E-08 -8.76E-12
40.046 -3.83E-02 2.45E-04 -2.17E-07 5.99E-11
33.933 -0.00842 0.0000299 -1.78E-08 3.69E-12
34.942 -4.00E-02 1.92E-04 -1.53E-07 3.93E-11
29.342 -3.54E-03 1.01E-05 -4.31E-09 2.59E-13

AR VALVE
 C D E Cp(Treff)
-1.96E-05 4.00E-09 -2.99E-13 38.4184753597
-3.85E-05 3.19E-08 -8.76E-12 28.7640420703
2.45E-04 -2.17E-07 5.99E-11 45.1630921134
0.0000299 -1.78E-08 3.69E-12 33.6378852467
1.92E-04 -1.53E-07 3.93E-11 36.3370088427
1.01E-05 -4.31E-09 2.59E-13 29.070164785
211.390668418
 C D E Cp(Treff) Hsensible
-1.96E-05 4.00E-09 -2.99E-13 6813.37061291 4,021,208.0528
-3.85E-05 3.19E-08 -8.76E-12 4837.60095492 31,406,334.8722
2.45E-04 -2.17E-07 5.99E-11 8406.94588266 19,846,904.2143
0.0000299 -1.78E-08 3.69E-12 5694.09852668 13,442,483.1114
1.92E-04 -1.53E-07 3.93E-11 6673.08183293 4,467.7163
1.01E-05 -4.31E-09 2.59E-13 4868.95221522 6,339.5625
37294.0500253 68,727,737.5295
 Cpg dT (J/mol) H sensibel (kJ/jam)
7180.4756088064 4237871.08929068
5085.1311278977 33013332.9640645
8885.7207647026 20977183.7899204
5989.4818077885 14139816.4555725
7049.7819799526 4719.9219751088
5118.3250994467 6664.2555126984
39308.9163885944 72379588.4763358
 Expansion Valve (EV-01)

Input Output
Komponen
Kg/Jam Kg/Jam
CO2 25983.28 25983.28
H2 12984.26 12984.26
CH3OH 75643.94 75643.94
H2O 42529.35 42529.35
CH4 10.74 10.74
N2 36.47 36.47
Sub Total 157188.04 157188.04
Total 157188.04 157188.04

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4)
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 27.437 4.23E-02
H2 2 25.399 2.02E-02
CH3OH 32.042 40.046 -3.83E-02
H2O 18.015 33.933 -0.00842
CH4 16.043 34.942 -4.00E-02

CP FASE CAIR
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4)
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 -338.956 5.28E+00
H2 2 50.607 -6.11E+00
 CH3OH 32.042 40.152 3.10E-01
H2O 18.015 92.053 -4.00E-02

ENTHALPY PENGUAPAN
Hvap= A( 1- T/TC)^n

Komponen BM A Tc
CO2 44.025 15.326 304.19
H2 2 0.659 33.18
CH3OH 32.042 52.723 512.58
H2O 18.015 52.053 647.13

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2

Komponen BM A B
CO2 44.025 35.0169 -1.51E+03
H2 2 3.4132 -4.13E+01
CH3OH 32.042 45.6171 -3.24E+03
H2O 18.015 29.8605 -3.15E+03

Expander Valve

INPUT
TEMPERATUR T (Reff)
P (bar) o
C K o
C
20 191.53687751 464.6868775104 25

INPUT

Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi

CO2 44.025 25983.28 590.193647353 0.0499916501
H2 2 12984.26 6492.130120883 0.5499081511
CH3OH 32.042 75643.94 2360.774589412 0.1999666004
H2O 18.015 42529.35 2360.774589412 0.1999666004
CH4 16.043 10.74 0.6695131833 5.671031695E-05
N2 28.013 36.47 1.3020383393 0.0001102876
Total 157188.04 11805.8444985827 1

MENENTUKAN SUHU KELUAR VALVE

P 1 bar
Treff 25 298.15 K
Komponen Kmol Xi A B
CO2 590.193647353 0.0499916501 27.437 4.23E-02
H2 6492.130120883 0.5499081511 25.399 2.02E-02
CH3OH 2360.774589412 0.1999666004 40.046 -3.83E-02
H2O 2360.774589412 0.1999666004 33.933 -0.00842
CH4 0.6695131833 5.671032E-05 34.942 -4.00E-02
N2 1.3020383393 0.0001102876 29.342 -3.54E-03
Total 11805.8444985827 1

Cp (25 C) 211.3906684178 kJ/kmol.K

R 8.314 kJ/kmol.k
Rules of Thumb Chemical Engineer Third Edition hal 129

Rumus
k=𝐶�/𝐶𝑣=𝐶�/
(𝐶� −�)
K 1.0409402029
K-1 0.0409402029
K-1/K 0.0393300237

Rumus

Δ𝐻=𝐶� x �1 x 〖 ((1−
ΔH
(𝑃2/𝑃1) 〗 ^((𝑘−1)/𝑘))x 0,5
5458.9590477186 kJ/kmol

Rumus
�2=�1 x 〖 (𝑃2/𝑃1) 〗 ^((𝑘−1)/𝑘)
+ 〖 (Δ𝐻/𝐶�) 〗 ^
T2 438.8628471094 K
165.7128471094 C

Pout 1.0000 bar

Tout 165.7128 438.8628 K
Treff 25.0000 298.1500 K
 Komponen Kmol Xi A B
CO2 590.193647353 0.0499916501 27.437 4.23E-02
H2 6492.130120883 0.5499081511 25.399 2.02E-02
CH3OH 2360.774589412 0.1999666004 40.046 -3.83E-02
H2O 2360.774589412 0.1999666004 33.933 -0.00842
CH4 0.6695131833 5.671032E-05 34.942 -4.00E-02
N2 1.3020383393 0.0001102876 29.342 -3.54E-03
Total 11805.8444985827 1

Hitungan panas yang diperlukan expander :

dHev= dHin - dHout

dHev= 11,045,691.2179

Neraca energi total EV

Aliran Panas Masuk Aliran Panas Keluar
Hin 68727737.5294733 Hout 57,682,046.3116
Hev 11,045,691.2179
TOTAL 68727737.5294733 TOTAL 68727737.5294733
ion Valve (EV-01)

CP FASE GAS
(sumber : yaws)

^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D E
-1.96E-05 4.00E-09 -2.99E-13
-3.85E-05 3.19E-08 -8.76E-12
2.45E-04 -2.17E-07 5.99E-11
0.0000299 -1.78E-08 3.69E-12
1.92E-04 -1.53E-07 3.93E-11

FASE CAIR
(sumber : yaws)

^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D
-2.33E-02 3.60E-05
3.09E-01 -4.15E-03
 -1.03E-03 1.46E-06
-2.11E-04 5.35E-07

NTHALPY PENGUAPAN
(sumber : yaws)

n
0.227
0.38
0.377
0.321

AN UAP MURNI
(sumber : yaws)

C D E
-1.13E+01 9.34E-03 1.71E-09
1.09E+00 -6.69E-10 1.46E-04
-1.40E+01 6.64E-03 -1.05E-13
-7.30E+00 2.42E-09 1.81E-06

Expander Valve

T (Reff)
K
298.15

A B C D E Cpg dT (J/mol)
27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13 6813.3706129104
25.399 2.02E-02 -3.85E-05 3.19E-08 -8.76E-12 4837.6009549167
40.046 -3.83E-02 2.45E-04 -2.17E-07 5.99E-11 8406.9458826564
33.933 -0.00842 0.0000299 -1.78E-08 3.69E-12 5694.0985266784
34.942 -4.00E-02 1.92E-04 -1.53E-07 3.93E-11 6673.081832925
29.342 -3.54E-03 1.01E-05 -4.31E-09 2.59E-13 4868.9522152158
37294.0500253026

UAR VALVE
 C D E Cp(Treff)
-1.96E-05 4.00E-09 -2.99E-13 38.4184753597
-3.85E-05 3.19E-08 -8.76E-12 28.7640420703
2.45E-04 -2.17E-07 5.99E-11 45.1630921134
0.0000299 -1.78E-08 3.69E-12 33.6378852467
1.92E-04 -1.53E-07 3.93E-11 36.3370088427
1.01E-05 -4.31E-09 2.59E-13 29.070164785
211.390668418
 C D E Cp(Treff) Hsensible
-1.96E-05 4.00E-09 -2.99E-13 5705.05610081 3,367,087.8685
-3.85E-05 3.19E-08 -8.76E-12 4082.9859508 26,507,276.0743
2.45E-04 -2.17E-07 5.99E-11 6978.35887007 16,474,332.2963
0.0000299 -1.78E-08 3.69E-12 4796.85150905 11,324,285.1518
1.92E-04 -1.53E-07 3.93E-11 5547.81592317 3,714.3359
1.01E-05 -4.31E-09 2.59E-13 4109.39118185 5,350.5849
31220.4595358 57,682,046.3116
H sensibel (kJ/jam)
4021208.05280136
31406334.8722271
19846904.214337
13442483.1113906
4467.7162605153
6339.5624566373
68727737.5294733
 Cooler (C-01)

Neraca Massa Cooler

Intlet
Komponen
Kg/Jam Kmol/Jam
CO2 25983.28 590.19
H2 12984.26 6492.13
CH3OH 75643.94 2360.77
H2O 42529.35 2360.77
CH4 10.74 0.67
N2 36.47 1.30
Total 157188.04 11805.84

Neraca Energi Cooler

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 *
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 27.437 4.23E-02
H2 2 25.399 2.02E-02
CH3OH 32.042 40.046 -3.83E-02
H2O 18.015 33.933 -0.00842
CH4 16.043 34.942 -4.00E-02

CP FASE CAIR
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +E/5 *
T reff = 25 C 298.15 K

Komponen BM A B
 CO2 44.025 -338.956 5.28E+00
H2 2 50.607 -6.11E+00
CH3OH 32.042 40.152 3.10E-01
H2O 18.015 92.053 -4.00E-02

ENTHALPY PENGUAPAN
Hvap= A( 1- T/TC)^n

Komponen BM A Tc
CO2 44.025 15.326 304.19
H2 2 0.659 33.18
CH3OH 32.042 52.723 512.58
H2O 18.015 52.053 647.13

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2

Komponen BM A B
CO2 44.025 35.0169 -1.51E+03
H2 2 3.4132 -4.13E+01
CH3OH 32.042 45.6171 -3.24E+03
H2O 18.015 29.8605 -3.15E+03

INPUT
P 1 Bar 1 bar
Tin 165.7128471094 C 438.8628471094 K
T reff 25 C 298.15 K
Komponen BM (kg/kmol) F3 (kg/jam) ni (kmol/jam) Xi
CO2 44.025 25983.275 590.194 0.0499916501
H2 2 12984.260 6492.130 0.5499081511
CH3OH 32.042 75643.939 2360.775 0.1999666004
H2O 18.015 42529.354 2360.775 0.1999666004
CH4 16.043 10.741 0.670 5.671031695E-05
N2 28.013 36.474 1.302 0.0001102876
Total 11805.844 0.9998897124

OUTPUT
P 1 Bar 1 bar
Tout 100 C 373.15 K
T reff 25 C 298.15 K
Komponen BM (kg/kmol) F3 (kg/jam) ni (kmol/jam) Xi
 CO2 44.025 25983.275 590.194 0.0499916501
H2 2 12984.260 6492.130 0.5499081511
CH3OH 32.042 75643.939 2360.775 0.1999666004
H2O 18.015 42529.354 2360.775 0.1999666004
CH4 16.043 10.741 0.670 5.671031695E-05
N2 28.013 36.474 1.302 0.0001102876
Total 11805.844 1

Q -27454082.128 Kj/Jam

Komponen BM (kg/kmol) A B C
H2O 18.015 92.053 -4.00E-02 -2.11E-04

fluida pendingin air TIN 30 303.15

TOUT 60 333.15
ʃCP dT -2256.6799942896 Kj/kmol

kebutuhan pendingin 12165.696 kmol/jam

219165.008 kg/jam

aliran panas masuk aliran panas keluar

Hin 57682046.312 H out 30227964.184
Q pendingin 27454082.128
Total 57682046.312 Total 57682046.312
 Cooler (C-01)

Komponen BM
CO2 44.025
H2 2
CH3OH 32.042
H2O 18.015
CH4 16.043
N2 28.013

CP FASE GAS
(sumber : yaws)

^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D E
-1.96E-05 4.00E-09 -2.99E-13
-3.85E-05 3.19E-08 -8.76E-12
2.45E-04 -2.17E-07 5.99E-11
0.0000299 -1.78E-08 3.69E-12
1.92E-04 -1.53E-07 3.93E-11

CP FASE CAIR
(sumber : yaws)

^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D
 -2.33E-02 3.60E-05
3.09E-01 -4.15E-03
-1.03E-03 1.46E-06
-2.11E-04 5.35E-07

ENTHALPY PENGUAPAN
(sumber : yaws)

n
0.227
0.38
0.377
0.321

ANAN UAP MURNI

(sumber : yaws)

C D E
-1.13E+01 9.34E-03 1.71E-09
1.09E+00 -6.69E-10 1.46E-04
-1.40E+01 6.64E-03 -1.05E-13
-7.30E+00 2.42E-09 1.81E-06

COOLER

A B C D E Cpg dT (J/mol)
27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13 5705.056
25.399 2.02E-02 -3.85E-05 3.19E-08 -8.76E-12 4082.986
40.046 -3.83E-02 2.45E-04 -2.17E-07 5.99E-11 6978.359
33.933 -0.00842 0.0000299 -1.78E-08 3.69E-12 4796.852
34.942 -4.00E-02 1.92E-04 -1.53E-07 3.93E-11 5547.816
29.342 -3.54E-03 1.01E-05 -4.31E-09 2.59E-13 4109.391
31220.460

A B C D E Cpg dT (J/mol)
 27.437 4.23E-02 -1.96E-05 4.00E-09 -2.99E-13 2968.269
25.399 2.02E-02 -3.85E-05 3.19E-08 -8.76E-12 2168.801
40.046 -3.83E-02 2.45E-04 -2.17E-07 5.99E-11 3556.784
33.933 -0.00842 0.0000299 -1.78E-08 3.69E-12 2539.193
34.942 -4.00E-02 1.92E-04 -1.53E-07 3.93E-11 2841.433
29.342 -3.54E-03 1.01E-05 -4.31E-09 2.59E-13 2184.912
16259.392

D
5.35E-07

Aliran Panas Masuk Aliran Panas Keluar

Komponen
Kj/Jam Kj/Jam
H2 3367087.87 1751853.37
CO2 26507276.07 14080136.25
CH3OH 16474332.30 8396764.84
H2O 11324285.15 5994462.52
CH4 3714.34 1902.38
N2 5350.58 2844.84
Q - 27454082.13
Total 57682046.31 57682046.31
H sensibel (kJ/jam)
3367087.868
26507276.074
16474332.296
11324285.152
3714.336
5350.585
57682046.312

H sensibel (kJ/jam)
 1751853.366
14080136.248
8396764.836
5994462.519
1902.377
2844.839
30227964.184
 Kondensor Parsial

Neraca Massa Kondensor Parsial

Intlet Output Fase Gas

Komponen
Kg/Jam Kmol/Jam Kg/Jam Kmol/Jam
CO2 25983.28 590.19 25983.28 590.19
H2 12984.26 6492.13 12984.26 6492.13
CH3OH 75643.94 2360.77 - -
H2O 42529.35 2360.77 - -
CH4 10.74 0.67 10.74 0.67
N2 36.47 1.30 36.47 1.30
Sub Total 157188.04 11805.84 39014.75
Total 157188.04 157188.04

Neraca Energi Kondensor Parsial

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4 (sumber : yaws)
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +
T reff = 25 C 298.15 K

Komponen BM A B C
CO2 44.025 27.437 4.23E-02 -1.96E-05
H2 2 25.399 2.02E-02 -3.85E-05
CH3OH 32.042 40.046 -3.83E-02 2.45E-04
H2O 18.015 33.933 -0.00842 0.0000299
CH4 16.043 34.942 -4.00E-02 1.92E-04

CP FASE CAIR
Cp = A + BT +CT^2 +DT ^3 +ET^4 (sumber : yaws)
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4) +
T reff = 25 C 298.15 K
 Komponen BM A B C
CO2 44.025 -338.956 5.28E+00 -2.33E-02
H2 2 50.607 -6.11E+00 3.09E-01
CH3OH 32.042 40.152 3.10E-01 -1.03E-03
H2O 18.015 92.053 -4.00E-02 -2.11E-04

ENTHALPY PENGUAPAN
Hvap= A( 1- T/TC)^n (sumber : yaws)

Komponen BM A Tc n
CO2 44.025 15.326 304.19 0.227
H2 2 0.659 33.18 0.38
CH3OH 32.042 52.723 512.58 0.377
H2O 18.015 52.053 647.13 0.321

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2 (sumber : yaws)

Komponen BM A B C
CO2 44.025 35.0169 -1.51E+03 -1.13E+01
H2 2 3.4132 -4.13E+01 1.09E+00
CH3OH 32.042 45.6171 -3.24E+03 -1.40E+01
H2O 18.015 29.8605 -3.15E+03 -7.30E+00

KONDENSOR PARSIAL

INPUT
TEMPERATUR T (Reff)
P (bar)
C o
K o
C K
1 100 373.15 25 298.15

Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi A

CO2 44.025 25983.275325 590.193647353 0.0499916501 27.437
H2 2 12984.260242 6492.13012088 0.5499081511 25.399
CH3OH 32.042 75643.939394 2360.77458941 0.1999666004 40.046
H2O 18.015 42529.354228 2360.77458941 0.1999666004 33.933
CH4 16.043 10.741 0.6695131833 5.6710317E-05 34.942
N2 28.013 36.474 1.3020383393 0.0001102876 29.342
Total 157188.04419 11805.8444986 1

OUTPUT
 TEMPERATUR T (Reff)
P (bar) o
C K o
C K
1 40 313.15 25 298.15

Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi A

CO2 44.025 25983.275325 590.193647353 0.0499916501 27.437
H2 2 12984.260242 6492.13012088 0.5499081511 25.399
CH3OH 32.042 75643.939394 2360.77458941 0.1999666004 40.152
H2O 18.015 42529.354228 2360.77458941 0.1999666004 92.053
CH4 16.043 10.741 0.6695131833 5.6710317E-05 34.942
N2 28.013 36.474 1.3020383393 0.0001102876 29.342
Total 157188.04419 11805.8444986 1

PANAS PENGEMBUNAN
Panas pengembunan adalah kebalikan dari panas penguapan

Temperatur Kondensor
∆H cond = (-) ∆H vap
313.15

∆H vap =A(1-(T/Tc)^n

KOMPONEN BM (kg/kmol) F2 (kg/jam) ni (kmol/jam) A Tc (K)

CH3OH 32.042 75643.939394 2360.77458941 52.723 512.58
H2O 18.015 42529.354228 2360.77458941 52.053 647.13
Total 118173.29362 4721.54917882

∆H Kondensor 143987603.27 Kj/jam

KEBUTUHAN PENDINGIN

Q 168280548.61 Kj/mol

Tin Tout
Fluida Pendingin o
C K o
C K
30 303.15 60 333.15

∫CP DT 2256.6799943 Kj/Kmol

Q 74569.965186 Kmol/Jam
Massa 1343377.9228 Kg/Jam

Aliran Panas Masuk Aliran Panas Keluar

Hin 30227964.184 Hout 5935018.83964
H cond 143987603.27 Q pendingin 168280548.61
TOTAL 174215567.45 TOTAL 174215567.45
ensor Parsial

Output Fase Cair

Kg/Jam Kmol/Jam
- -
- -
75643.94 2360.77
CO2
42529.35 2360.77 H2
CH3OH
Kondensor P
- -
H2O FASE
- - GAS Cp
118173.29 = A + BT
+CT^2 +DT
157188.04 ^3 +ET^4
(sumber :
yaws)
Dengan Cp
= kapasitas
panas
cairan,
j/mol.K T =
sumber : yaws) suhu,
Kelvin ʃCP
dT = A(Tin-
Treff) +
eff^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5) B/2 *
(Tin^2 -
Treff^2) +
C/3 (Tin^3
- Treff^3) +
D E D/4*
4.00E-09 -2.99E-13 (Tin^4-
3.19E-08 -8.76E-12 Treff^4)
+E/5 *
-2.17E-07 5.99E-11 (Tin^5-
-1.78E-08 3.69E-12 Treff^5) T
reff = 25 C
-1.53E-07 3.93E-11 298.15 K
H2
CAIR
sumber : yaws)

eff^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

 D
3.60E-05
-4.15E-03
1.46E-06
5.35E-07

HALPY PENGUAPAN
sumber : yaws)

P MURNI
sumber : yaws)

D E
9.34E-03 1.71E-09
-6.69E-10 1.46E-04
6.64E-03 -1.05E-13
2.42E-09 1.81E-06

NDENSOR PARSIAL

B C D E Cpg dT (J/mol)
0.042315 -0.000019555 0.000000004 -2.987E-13 2968.26876029
0.020178 -0.000038549 3.188E-08 -8.759E-12 2168.80068412
-0.038287 0.00024529 -2.1679E-07 5.9909E-11 3556.78380872
-0.00842 0.0000299 -1.78E-08 3.69E-12 2539.19308751
-4.00E-02 1.92E-04 -1.53E-07 3.93E-11 2841.43347875
-3.54E-03 1.01E-05 -4.31E-09 2.59E-13 2184.91190818
16259.3917276
 B C D E Cpg dT (J/mol)
0.042315 -0.000019555 0.000000004 -2.987E-13 579.823981782
0.020178 -0.000038549 3.188E-08 -8.759E-12 431.980360564
3.10E-01 -1.03E-03 1.46E-06 676.044046517
-4.00E-02 -2.11E-04 5.35E-07 504.670928502
-4.00E-02 1.92E-04 -1.53E-07 3.93E-11 549.391237854
-3.54E-03 1.01E-05 -4.31E-09 2.59E-13 436.211054388
3178.12160961

PANAS PENGEMBUNAN

emperatur Kondensor
K

n ∆Hv (kJ/jam) Hv
0.377 8.9386778634 21102.2035629182
0.321 52.053 122885.399702663
60.9916778634 143987.603265581

TUHAN PENDINGIN

Aliran Panas Masuk Aliran Panas Keluar

Komponen
Komponen
Kj/Jam Kj/Jam
CO2 1751853.37 342208.43
H2 14080136.25 2804472.71
CH3OH 8396764.84 1595987.61
H2O 5994462.52 1191414.30
CH4 1902.38 367.82
N2 2844.84 567.96
Hkondensor 143987603.27
Qpendingin - 168280548.61
Total 174215567.45 174215567.45
 Intlet
Komponen
Kg/Jam
CO2 25983.28
H2 12984.26
CH3OH 75643.94
H2 O 42529.35
Kondensor Parsial CO2 (g)
H2 (g)
CH3OH (l)
H2O (l)P
FASE GAS
Cp = A + Sub Total 157188.04
BT +CT^2 Total 157188.04
+DT ^3
+ET^4
(sumber :
yaws)
Dengan Cp
= kapasitas
panas
cairan,
j/mol.K T =
suhu,
Kelvin ʃCP
dT = A(Tin-
Treff) + B/2
* (Tin^2 -
Treff^2) +
C/3 (Tin^3
- Treff^3) +
D/4*
(Tin^4-
Treff^4)
+E/5 *
(Tin^5-
Treff^5) T
reff = 25 C
298.15 K
H2
H sensibel (kJ/jam)
1751853.3659616
14080136.2475971
8396764.83565061
5994462.51860461
1902.3771735499
2844.8390725407
30227964.18406
H sensibel (kJ/jam)
342208.430630853
2804472.71044955
1595987.60633944
1191414.30402219
367.8246765435
567.963516858
5935018.83963543
Output Fase Gas Output Fase Cair
Kg/Jam Kg/Jam
25983.28 -
12984.26 -
- 75643.94
- 42529.35

39014.75 118173.29
157188.04
 Separ

Neraca Massa Separator Drum

Input Output Top

Komponen
Kg/Jam Kmol/Jam Kg/Jam
CO2 25983.28 590.19 25983.28
H2 12984.26 6492.13 12984.26
CH3OH 75643.94 2360.77 0.00
H2 O 42529.35 2360.77 0.00
CH4 10.74 0.67 10.74
N2 36.47 1.30 36.47
Sub Total 157188.04 11805.84 39014.75
Total 157188.04 15718

Neraca Energi Separator Drum

CP FASE GAS
Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 27.437 4.23E-02
H2 2 25.399 2.02E-02
CH3OH 32.042 40.046 -3.83E-02
H2O 18.015 33.933 -0.00842
CH4 16.043 34.942 -4.00E-02

CP FASE CAIR
 Cp = A + BT +CT^2 +DT ^3 +ET^4
Dengan Cp = kapasitas panas cairan, j/mol.K
T = suhu, Kelvin
ʃCP dT = A(Tin-Treff) + B/2 * (Tin^2 - Treff^2) + C/3 (Tin^3 - Treff^3) + D/4* (Tin^4-Treff^4
T reff = 25 C 298.15 K

Komponen BM A B
CO2 44.025 -338.956 5.28E+00
H2 2 50.607 -6.11E+00
CH3OH 32.042 40.152 3.10E-01
H2O 18.015 92.053 -4.00E-02

ENTHALPY PENGUAP
Hvap= A( 1- T/TC)^n

Komponen BM A Tc
CO2 44.025 15.326 304.19
H2 2 0.659 33.18
CH3OH 32.042 52.723 512.58
H2O 18.015 52.053 647.13

TEKANAN UAP MURNI

log Psat = A + B/T+C log T + D T + E T^2

Komponen BM A B
CO2 44.025 35.0169 -1.51E+03
H2 2 3.4132 -4.13E+01
CH3OH 32.042 45.6171 -3.24E+03
H2O 18.015 29.8605 -3.15E+03

SEPARATOR DRUM

INPUT
TEMPERATUR T (Reff)
P (bar) o
C K o
C
1 40 313.15 25

FASE GAS
Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi
CO2 44.025 25983.27532472 590.193647353 0.0833101418
H2 2 12984.26024177 6492.130120883 0.9164115594
 CH4 16.043 10.74 0.6695131833 9.45066733E-05
N2 28.013 36.47 1.3020383393 0.0001837922
Total 7084.2953197587 1

FASE CAIR
Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi
CH3OH 32.042 75643.93939394 2360.774589412 0.5
H2O 18.015 42529.35422826 2360.774589412 0.5
Total 4721.549178824 1

OUTPUT
TEMPERATUR T (Reff)
P (bar) o
C K o
C
1 40 313.15 25

FASE GAS
Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi
CO2 44.025 25983.27532472 590.193647353 0.0833101418
H2 2 12984.26024177 6492.130120883 0.9164115594
CH4 16.043 10.741 0.6695131833 9.45066733E-05
N2 28.013 36.474 1.3020383393 0.0001837922
Total 39014.75056648 7084.2953197587 1

FASE CAIR
Komponen BM (Kg/mol) F3 (kg/jam) ni (kmol/jam) Xi
CH3OH 32.042 75643.93939394 2360.774589412 0.5
H2O 18.015 42529.35422826 2360.774589412 0.5
Total 118173.2936222 4721.549178824 1

aliran panas masuk aliran panas keluar

Hin 8671569.571188 Hout (g) 3147616.9292738
Hout (l) 5523952.6419139
Total 8671569.571188 Total 8671569.5711877
 Separator Drum (KOD)

Output Top Output Bottom

Kmol/Jam Kg/Jam Kmol/Jam
590.19 0.00 0.00
6492.13 0.00 0.00
0.00 75643.94 2360.77
0.00 42529.35 2360.77
0.67 0.00 0.00
1.30 0.00 0.00
7084.30 118173.29 4721.55
157188.04

CP FASE GAS
(sumber : yaws)

ff^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D E
-1.96E-05 4.00E-09 -2.99E-13
-3.85E-05 3.19E-08 -8.76E-12
2.45E-04 -2.17E-07 5.99E-11
0.0000299 -1.78E-08 3.69E-12
1.92E-04 -1.53E-07 3.93E-11

P FASE CAIR
 (sumber : yaws)

ff^3) + D/4* (Tin^4-Treff^4) +E/5 * (Tin^5-Treff^5)

C D
-2.33E-02 3.60E-05
3.09E-01 -4.15E-03
-1.03E-03 1.46E-06
-2.11E-04 5.35E-07

ENTHALPY PENGUAPAN
(sumber : yaws)

n
0.227
0.38
0.377
0.321

NAN UAP MURNI

(sumber : yaws)

C D E
-1.13E+01 9.34E-03 1.71E-09
1.09E+00 -6.69E-10 1.46E-04
-1.40E+01 6.64E-03 -1.05E-13
-7.30E+00 2.42E-09 1.81E-06

SEPARATOR DRUM

T (Reff)
K
298.15

A B C D
27.437 4.23E-02 -1.96E-05 4.00E-09
25.399 2.02E-02 -3.85E-05 3.19E-08
 34.942 -4.00E-02 1.92E-04 -1.53E-07
29.342 -3.54E-03 1.01E-05 -4.31E-09

A B C D
40.152 3.10E-01 -1.03E-03 1.46E-06
92.053 -4.00E-02 -2.11E-04 5.35E-07

T (Reff)
K
298.15

A B C D
27.437 4.23E-02 -1.96E-05 4.00E-09
25.399 2.02E-02 -3.85E-05 3.19E-08
34.942 -4.00E-02 1.92E-04 -1.53E-07
29.342 -3.54E-03 1.01E-05 -4.31E-09

A B C D
40.152 3.10E-01 -1.03E-03 1.46E-06
92.053 -4.00E-02 -2.11E-04 5.35E-07

Aliran Panas Masuk

Komponen
Kj/Jam
CO2 342208.43
H2 2804472.71044955
CH3OH 2853933.19
H2O 2670019.45
CH4 367.82
N2 567.96
Total 8671001.61
Komponen BM
CO2 44.025
H2 2
CH3OH 32.042
H2O 18.015
 E Cpg dT (J/mol) H sensibel (kJ/jam)
-2.99E-13 579.8239817823 342208.430630853
-8.76E-12 431.9803605643 2804472.71044955
 3.93E-11 549.3912378538 367.8246765435
2.59E-13 436.2110543878 567.963516858
1997.4066345883 3147616.92927381

Cpg dT (J/mol) H sensibel (kJ/jam)

1208.8969441428 2853933.18695006
1130.9929660116 2670019.45496382
2339.8899101543 5523952.64191387

E Cpg dT (J/mol) H sensibel (kJ/jam)

-2.99E-13 579.8239817823 342208.430630853
-8.76E-12 431.9803605643 2804472.71044955
3.93E-11 549.3912378538 367.8246765435
2.59E-13 436.2110543878 567.963516858
1997.4066345883 3147616.92927381

Cpg dT (J/mol) H sensibel (kJ/jam)

1208.8969441428 2853933.18695006
1130.9929660116 2670019.45496382
2339.8899101543 5523952.64191387

Aliran Panas Keluar

Kj/Jam
342208.43
2804472.71044955
2853933.19
2670019.45
367.82
567.96
8671001.61
 Input Output Top Output Bottom
Komponen
Kg/Jam Kg/Jam Kg/Jam
CO2 25983.28 25983.28 0.00
H2 12984.26 12984.26 0.00
CH3OH 75643.94 0.00 75643.94
H2 O 42529.35 0.00 42529.35
CH4 10.74 10.74 0.00
N2 36.47 36.47 0.00
Total 157188.04 39014.75 118173.29
Kg/Jam Total 157188.04 157188.04
Neraca Massa Absorber

Komponen BM (Kg/mol) Input (Kg/Jam) Input (Kmol/Jam)

CO2 44.025 25983.275324716 590.193647353
H2 2 12984.260241766 6492.130120883
CH4 16.043 10.741 0.6695131833
N2 28.013 36.474 1.3020383393
Total 39014.750566482 7084.2953197587

ABSORBER
Inlet Output Top Output Bottom
Komponen
Kg/Jam Kmol/Jam Kg/Jam Kmol/Jam Kg/Jam
CO2 25983.27532472 590.193647353 25983.275324716 590.193647 0
H2 12984.26024177 6492.130120883 12984.260241766 6492.13012 0
CH4 10.741 0.6695131833 0.00 0 10.74
N2 36.474 1.3020383393 36.474 1.30203834 0
CH2
Total

PSA (PRESSURE SWING ADSORPTION)

Inlet Output Top Output Bottom

Komponen
Kg/Jam Kmol/Jam Kg/Jam Kmol/Jam Kg/Jam
CO2 25983.27532472 590.193647353 25983.275324716 590.193647 0
H2 12984.26024177 6492.130120883 12984.260241766 6492.13012 0
CH4 10.741 0.6695131833 0.010741 0.00066951 10.730259
N2 36.474 1.3020383393 36.437526 1.3007363 0.036474
Sub Total 39014.75056648 39003.983833482 10.766733
Total 39014.7505664819 39014.7505664819

Perhitungan ke IPAL :

Neraca massa total : 39003.983833482

Rencana untuk pembuangan ke ipal 1-5%, diambil 5% 0.05

Komponen RECYCLE IPAL

CO2 24684.11155848 1299.1637662358
H2 12335.04722968 649.2130120883
CH4 0.01020395 0.00053705
N2 34.6156497 1.8218763
Total 37053.78464181 1950.1991916741
Bahan Recycle :
Komponen Kebutuhan Bahan
CO2 105232.27
H2 5370.76
CH4 10.73
N2 1.86
Total 110615.62

Neraca Energi
 Output Bottom
Kmol/Jam
0
0
0.6695131833
0

Output Bottom BM (Kg/mol)

Kmol/Jam 44.025
0 2
0 16.043
0.6688436701 28.013
0.0013020383

819