NERACA PANAS Pra Rancangan Pabrik Stirena Dari Etilbenzen Melalui Proses Dehidrogenasi Katalitik Menggunakan Katalis Shell – 105 Dengan Kapasitas 100.000 Ton / Tahun

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