BAB IV NERACA PANAS
1. Neraca Panas Di Mixer M – 01
Tabel 4.1 Neraca Panas di Mixer
Komponen Input
Output Alur 3 Fresh Feed Alur 1
Recycle Feed Alur 2 Q kJjam
Benzen 309,720
0,000 2.440,523
Toluen 298,330
0,000 2.342,363
Etilbenzen 120.802,703
1.184.551,172 1.343.766,778
Styrene 0,000
64.338,551 21.750,472
Subtotal 121.410,753
1.248.889,723 1.370.300,476
Total 1.370.300,476 kJjam
1.370.300,476 kJjam
2. Neraca Panas Di Vaporizer
V – 01
Tabel 4.2 Neraca Panas di Vaporizer
Komponen Input Vaporizer
Output Vaporizer Feed Mixer
Feed WHB Feed Mixer
Feed WHB n.Cp.dT
n.Cp.dT n.Cp.dT
n.Hv
2
Q total n.Cp.dT
Benzen 2.440,523
113.184,646 9.263,146723
11.246,11612 20.509,26284 90.043,287
Toluen 2.342,363
197.192,918 8.835,134704
11.691,81497 20.526,94967 157.107,294
Etilbenzen 1.343.766,778
2.177.651,896 5.003.881,473 6.513.750,704 11.517.632,18 1.736.628,426 Stirena
21.750,472 6.349.787,334
79.628,14482 105.029,261 184.657,4058 4.928.769,375
Air 43.805.822,632
9.263,146723 11.246,11612 20.509,26284 35.626.705,292
CO
2
126.987,780 103.666,274
H
2
1.302.621,319 1.057.303,828
Total 1.370.300,476 54.073.248,525 5.101.607,899 6.641.717,896 11.743.325,8 43.700.223,205
Jumlah 55.443.549,001 kJjam
55.443.549,001 kJjam
Universitas Sumatera Utara
3. Neraca Panas Di Furnace
F – 01
Tabel 4.3 Neraca Panas Alur Umpan di Furnace
Komponen Input Furnace Output Vaporizer
Output Furnace kmol
n.Cp.dT n.Hvap
Q total kJ kmol
Cp.dT n.Cp.dT
Benzen 0,448 9.263,146723 11.246,11612 20.509,26284
0,448 87.144,448 39040,7127
Toluen 0,378 8.835,134704 11.691,81497 20.526,94967
0,378 107.215,215 40527,35127
Etilbenzen 186,630 5.003.881,473 6.513.750,704 11.517.632,18 186,630 129.433,167 24.156.111,96
Stirena 2,969 79.628,14482
105.029,261 184.657,4058 2,969 246.793,544
732.730,0321 190,425 5.101.607,899 6.641.717,896 11.743.325,8 190,425
24.968.410,06 Jumlah
11.743.325,8 kJjam
24.968.410,06 kJjam
Beban panas furnace 1 = Q
output
- Q
input
= 24.968.410,06 kJjam – 11.743.325,8 kJjam
= 13.225.084,26
kJjam Tabel 4.4 Neraca Panas Alur Steam di Furnace
Komponen Input Furnace
Output Furnace kmoljam
Cp.dT Q kJ
kmoljam Cp .dT
Q kJ H
2
O steam
5.187,576 6.460,178 33.512.664,3485 5.187,576 35.302,835 183.136.139,5780
Jumlah
33.512.664,3485 kJjam 183.136.139,5780 kJjam
Beban panas furnace 2 = Q
output
- Q
input
= 183.136.139,5780 kJjam – 33.512.664,3485 kJjam
= 149.623.475,2294 kJjam Beban panas furnace total = beban panas furnace 1 + beban furnace 2
= 13.225.084,26 kJjam +149.623.475,2294 kJjam
=162.848.559,4894 kJjam Spesifikasi bahan bakar yang digunakan Yaws, C. L, 1998 :
Hv = 41.123,5988 kJkg Eff = 78
M
fuel
= Q Hv . Eff M
fuel
= 162.848.559,4894 kJjam 41.123,5988 kJkg x 0,78 = 5.076,8953 kgjam
Kebutuhan fuel bahan bakar pada furnace = 5.076,8953 kgjam
Universitas Sumatera Utara
4. Neraca Panas Di Bed Reaktor I R – 01
Tabel 4.5 Neraca Panas di Bed Reaktor I
Komponen Input Bed Reaktor 1
Output Bed Reaktor 1 kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Q
reaksi
Benzen 0,448 81.309,838
36.426,807 3,067 70.520,1817
216.285,397 Toluen
0,378 100.032,727 37.812,371
4,117 86.765,21595 357.212,394
Etilbenzen 186,630 120.793,733 22.543.734,420 105,625 104.841,5482 11.073.888,527
Stirena 2,969 222.496,875
660.593,222 77,615 178.929,756 13.887.633,013
Steam 3.318,588 25.703,378 85.298.922,577 3.300,631 21.449,78504 70.797.825,454
CO
2
0,000 0,000
8,977 22.076,07912 198.176,962
H
2
0,000 0,000
101,578 20.268,46228 2.058.829,862 Subtotal
3.509,013 108.577.489,113 3.601,61
98.589.851,271 9.967.637,832 Jumlah
108.577.489,113 kJjam 108.577.489,113 kJjam
5. Neraca Panas Di Bed Reaktor II R – 01
Tabel 4.6 Neraca Panas di Bed Reaktor II
Komponen Input Bed Reaktor 2
Output Bed Reaktor 2 kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Q
reaksi
Benzen 3,067 76,691.985
235.214,317 4,342 68.334,77525
296.709,594 Toluen
4,117 90,154.278 371.165,162
6,120 84.079,16264 514.564,475
Etilbenzen 105,625 117,483.963 12.409.243,583 55,684 101.606,2999
5.657.845,205 Stirena
77,615 191,537.322 14.866.169,213 124,280 171.577,9835 21.323.711,793 Steam
5.169,620 22,297.464 115.269.414,059 5.160,517 20.783,90623 107.255.701,421 CO
2
8,977 24,378.570 218.846,423
13,529 21.469,25057 290.457,491
H
2
101,578 22,604.703 2.296.140,474 161,897 19.650,55937
3.181.366,610 Subtotal 5.470,599
145.666.193,891 5.526,369 138.520.356,407 7.145.837,484
Jumlah 145.666.193,891 kJjam
145.666.193,891 kJjam
6. Neraca Panas Di Waste Heat Boiler WHB
Tabel 4.7 Neraca Panas di Waste Heat Boiler
Komponen Input Waste Heat Boiler
Output Waste Heat Boiler kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Benzen
4,342 68.334,77525
296.709,594 4,342 26.067,399
113.184,646 Toluen
6,120 84.079,16264
514.564,475 6,120 32.221,065
197.192,918 Etilbenzen
55,684 101.606,2999
5.657.845,205 55,684 39.107,318
2.177.651,896 Stirena
124,280 171.577,9835
21.323.711,793 124,280 51.092,592
6.349.787,334
Universitas Sumatera Utara
Air 5.160,517
20.783,90623 107.255.701,421 5.160,517
8.488,650 43.805.822,632 CO
2
13,529 21.469,25057
290.457,491 13,529
9.386,339 126.987,780
H
2
161,897 19.650,55937
3.181.366,610 161,897
8.045,988 1.302.621,319
Total 5.526,369
138.520.356,407 5.526,369
54.073.248,525
Panas yang diambil WHB = panas input WHB – panas output WHB = 138.520.356,407 kJjam – 54.073.248,525 kJjam
= 84.447.107,882 kJjam Panas yang dibutuhkan dari air umpan :
o Panas yang dibutuhkan untuk mengubah fase dari cair menjadi cair jenuh.
o Panas yang dibutuhkan untuk mengubah dari kondisi cair jenuh menjadi uap
jenuh. Dari steam table untuk T = 473 K diperoleh λ = 34.923,879 kJkmol.
Sehingga panas yang dibutuhkan dari air umpan = 13.090,751 + 34.923,879 = 31.658,022 kJkmol.
Jumlah air yang dibutuhkan di WHB adalah 31.658,022 kgjam.
7. Neraca Panas Di Cooler IV CL – 04
Tabel 4.8 Neraca Panas di Cooler IV
Komponen Input Cooler IV
Output Cooler IV kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Benzen
4,342 20.737,745
90.043,287 4,342 15.310,4596
66.478,016 Toluen
6,120 25.671,126
157.107,294 6,120 19.001,9527
116.291,951 Etilbenzen
55,684 31.187,207
1.736.628,426 55,684 23.121,0178
1.287.470,755 Stirena
124,280 39.658,588
4.928.769,375 124,280 28.448,9678
3.535.637,718 Air
5.160,517 6.903,709
35.626.705,292 5.160,517 5.289,2003 27.295.008,065
CO
2
13,529 7.662,523
103.666,274 13,529 5.887,1623
79.647,419 H
2
161,897 6.530,719
1.057.303,828 161,897 4.984,4218
806.962,936 Total
5.526,369 43.700.223,205
5.526,369 33.187.496,859
Panas yang diambil cooler IV = panas input – panas output = 43.700.223,205 – 33.187.496,859
= 10.512.726,346 kJjam
Universitas Sumatera Utara
Kebutuhan air pendingin di cooler IV = 167.394,770 kgjam
8. Neraca Panas Di Drum Separator DS – 01
Tabel 4.9 Neraca Panas di Drum Separator
Komponen Input Drum Separator
Output Drum Separator kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Benzen
4,342 15.310,4596
66.478,016 4,342 10.953,583
47,560.457 Toluen
6,120 19.001,9527
116.291,951 6,120 12.437,692
76,118.675 Etilbenzen
55,684 23.121,0178
1.287.470,755 55,684 14.457,642
805,059.337 Stirena
124,280 28.448,9678
3.535.637,718 124,280 14.686,526
1,825,241.451 Air
5.160,517 5.289,2003
27.295.008,065 5.160,517
5.705,827 29,445,017.233 CO
2
13,529 5.887,1623
79.647,419 13,529
3.001,762 40.610,838
H
2
161,897 4.984,4218
806.962,936 161,897
2.523,822 408.599,210
Total 5.526,369
33.187.496,859 5.526,369
32.648.207,202
Beban panas drum separator = panas input drum – panas output drum = 33.187.496,859 kJjam – 32.648.207,202 kJjam
= 539,289.657 kJjam Kebutuhan air pendingin di kondensor = 8.587,1414 kgjam
9. Neraca Panas Di Dekanter D – 01
Tabel 4.10 Neraca Panas di Dekanter
Komponen Input Dekanter
Output Dekanter Hasil atas
Hasil bawah kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT kmol
Cp.dT n.Cp.dT
Benzen 4,342 10.953,583
47.560,457 3,515 10.953,583
38.501,844 0,826 10.953,583
9.047,660 Toluen
6,120 12.437,692 76.118,675
5,616 12.437,692 69.850,078
0,504 12.437,692 6.268,597
Etilbenzen 55,684 14.457,642
805.059,337 55,600 14.457,642 803.844,895 0,084 14.457,642
1.214,442 Stirena
124,280 14.686,526 1.825.241,451 124,00 14.686,526 1.821.129,224 0,280 14.686,526
4.112,227 Air
5.160,517 5.705,827 29.445.017,233 5.160,517 5.705,827 29.445.017,233
Total 5.350,943
32.198.997,153 188,731 2.733.326,042 5.162,211
29.465.660,158
Panas output dekanter = panas hasil atas + panas hasil bawah = 2.733.326,042 kJjam + 29.465.660,158 kJjam
= 32.198.997,153 kJjam
Universitas Sumatera Utara
10. Neraca Panas Di Kolom Destilasi I D – 01
Tabel 4.11 Neraca Panas di Kolom Destilasi I
Komponen Input Kolom Destilasi I
Output Kolom Destilasi I Hasil atas
Hasil bawah kmol
Cp.dT n.Cp.dT
kmol Q
Lo
Q
D
Q
V
kmol Q
W
Toluen 5,616 12.437,692
42.109,249 5,616 1.009.303,579 60.170,05
2.211.104,767 0,000
0,000 Benzen
3,515 10.953,583 65.761,368 3,515
556.932,781 84.754,91
4.255.813,962 0,000
0,000 Etilbenzen 55,600 14.457,642 803.845,008 55,376 11.549.138,653 1.100.043,69
47.175.800,06 0,224
5,364.085 Stirena
124,000 14.686,526 1.821.123,457 2,983 630.669,821
60.070,66 2.649.555,335 121,017 2,932,262.725
Total 188,731
2.732.839,082 67,490 13.746.044,834 1.305.039,31 56.292.274,135 121,241 2,937,626.810
Neraca Panas di kondensor :
Q
input
= Q
output
Q
V
= Q
Lo
+ Q
D
+ Q
C
Q
C
= 56.292.274,135 – 13.746.044,834 – 1.305.039,31 = 41.241.189,991
kJjam
Kebutuhan air pendingin di kondensor I = 656.685,9334 kgjam
Neraca panas di reboiler :
Q
input
= Q
output
Q
F
+ Q
R
= Q
D
+ Q
W
+ Q
C
Q
R
= 1.305.039,31 + 2.937.626,810 + 41.241.189,991 – 2.733.326,042 = 42.750.530,07 kJjam
Kebutuhan steam di reboiler I = 22.033,908 kgjam
11. Neraca Panas Di Kolom Destilasi II D – 02
Tabel 4.12 Neraca Panas di Kolom Destilasi II
Komponen Input Kolom Destilasi II
Output Kolom Destilasi II Hasil atas
Hasil bawah kmol
Cp.dT n.Cp.dT
kmol Q
Lo
Q
D
Q
V
kmol Q
W
Toluen 3,515 17.118,080
53.047,280 5,616 109.710,4271 71.163,520272 993.528,018 0,000
0,000 Benzen
5,616 15.091,687 96.135,137 3,515 60.477,1075 39.228,092455 574.616,0348 0,000
0,000 Etilbenzen 55,376 19.864,990 1.100.043,686
0,014
324,0236 206,196844
2.917,0066 55,362 1.196.592,386 Stirena
2,983 20.137,666 60.070,658 0,011
254,3226 164,561683
2.368,5927 2,969 65.002,437
Total 67,490
1.309.296,761 9,156 170.765,8808 110.762,371254 1.570.429,6522 58,331 1.261.594,823
Neraca panas di sekitar kondensor :
Universitas Sumatera Utara
Q
input
= Q
output
Q
V
= Q
Lo
+ Q
D
+ Q
C
Q
C
= 1.570.429,6522 – 170.765,8808 – 110.762,371254 = 1.288.901,40011 kJjam
Kebutuhan air pendingin di kondensor II = 10.170,775 kgjam
Neraca panas di reboiler :
Q
input
= Q
output
Q
F
+ Q
R
= Q
D
+ Q
W
+ Q
C
Q
R
= 110.762,371254 + 1.261.594,823 + 1.288.901,40011 – 1.309.296,761 = 1.351.961,833 kJjam
Kebutuhan steam di reboiler II = 696,8106 kgjam
12. Neraca Panas Di Kolom Destilasi III D – 03
Tabel 4.13 Neraca Panas di Kolom Destilasi III
Komponen Input Kolom Destilasi III
Output Kolom Destilasi III Hasil atas
Hasil bawah kmol
Cp.dT n.Cp.dT
kmol Q
Lo
Q
D
Q
V
kmol Q
W
Toluen 5,616 11.160.197
71.163,520 3,501 53,84127 31.400,0909
1.447,9744 5,602 69.841,03032 Benzen
3,515 12.671.567 39.228,092 0,014 11.845,85404
110,4724 304.533,8882 0,014 198,10797
Etilbenzen 0,014 14.728.346 206,197 0,000
0,000 0,0000
0,0000 0,014 230,14684
Stirena 0,011 14.960.153
164,562 0,000 0,000
0,0000 0,0000 0,014
233,62689 Total
9,156 110.762,371 3,515 11.899,69531 31.510,5633 305.981,8625 5,644 70.502,91202
Neraca Panas di kondensor :
Q
input
= Q
output
Q
V
= Q
Lo
+ Q
D
+ Q
C
Q
C
= 305.981,8625 – 11.899,69531 – 31.510,5633 = 262.571,6039 kJjam
Kebutuhan air pendingin di kondensor III = 4.180,9433 kgjam
Neraca panas di reboiler :
Q
input
= Q
output
Q
F
+ Q
R
= Q
D
+ Q
W
+ Q
C
Q
R
= 31.510,5633 + 70.502,91202 + 262.571,6039 – 110.762,371
Universitas Sumatera Utara
= 253.822,7082 kJjam Kebutuhan steam di reboiler III= 130,824 kgjam
13. Neraca Panas Di Cooler I CL – 01
Tabel 4.14 Neraca Panas di Cooler I
Komponen Input Cooler I
Output Cooler I kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Toluen
0,000 18.233,520
0,000 0,000
2.790,968 0,000
Benzen 0,000
20.664,308 0,000
0,000 3.180,717
0,000 Etilbenzen
0,224 23.946,809
5.364,085 0,224
3.707,170 830,406
Stirena 121,017
24.230,172 2.932.262,725
121,017 3.774,273
456.751,196 Total
121,241 2.937.626,810
121,241 457.581,602
Panas yang diambil cooler I = panas input – panas output = 2.937.626,810 – 457.581,602
= 2.480.045,208 kJjam Kebutuhan air pendingin di cooler I = 39.489,908 kgjam
14. Neraca Panas Di Cooler II CL – 02
Tabel 4.15 Neraca Panas di Cooler II
Komponen Input Cooler II
Output Cooler II kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Toluen
0,014 7.890,886
110,472 0,014
2.790,968 39,074
Benzen 3,501
8.968,892 31.400,091
3,501 3.180,717
11.135,690 Etilbenzen
0,000 10.436,958
0,000 0,000
3.707,170 0,000
Stirena 0,000
10.614,596 0,000
0,000 3.774,273
0,000 Total
3,515 31.510,563
3,515 11.174,764
Panas yang diambil cooler II = panas input – panas output = 31.510,563 – 11.174,764
= 19.975,799 kJjam Kebutuhan air pendingin di cooler II = 318,076 kgjam
15. Neraca Panas Di Cooler III CL – 03
Universitas Sumatera Utara
Tabel 4.16 Neraca Panas di Cooler III
Komponen Input Cooler III
Output Cooler III kmol
Cp.dT n.Cp.dT
kmol Cp.dT
n.Cp.dT Toluen
5,602 12.467,160
69.841,030 5,602
2.790,968 15.635,0027
Benzen 0,014
14.150,569 198,108
0,014 3.180,717
44,5300 Etilbenzen
0,014 16.439,060
230,147 0,014
3.707,170 51,9004
Stirena 0,014
16.687,635 233,627
0,014 3.774,273
52,8398 Total
5,644 70.502,912
5,644 15.784,2730
Panas yang diambil cooler III = panas input – panas output = 70.502,912 – 15.784,273
= 54.718,639 kJjam Kebutuhan air pendingin di cooler III = 871,288 kgjam
Universitas Sumatera Utara
BAB V SPESIFIKASI PERALATAN