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22 BAB 3 SPESIFIKASI ALAT Tabel 3.1 Spesifikasi Heater 1A & 1B SPESIFIKASI ALAT Nama Alat Heater Kode Alat Fungsi Memanaskan Udara Sebelum Masuk Reaktor Jenis
Shell and tube heat exchanger Tube Side Fluida Udara Laju alir fluida 564806,6267 (lb/jam) Temperatur masuk 87,8 (F) Temperatur keluar 177,8 (F) 12708149,1 329,521 940,620
Shell Side Fluida Steam Laju alir fluida 10008,94 (lb/jam) Temperatur masuk 464 (F) Temperatur keluar 464 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF)
8,550 40,738 Allowable 0,02
Dirt factor, RD (hr)(ft2)(oF)/Btu Shell Side Shell ID (in) 25 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,0825 diameter, de
Corrected 0,0092 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft)
1 0,810 226 16
BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
H-01A & 1B
Allowab le
Calculat ed
3
0,218
Pressure Drop, ∆P (psi)
13 0,515 1,25 6 Allowab Calculat le ed 3
0,37
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
23
GAMBAR ALAT
T in
t out
T out
t in
Gambar 3.1 2-6 Heat Exchanger (kern,1965)
Tabel 3.2 Spesifikasi Heater 2 Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
24 SPESIFIKASI ALAT Heater Kode Alat H-02 Memanaskan LPG Butana Sebelum Masuk Reaktor
Nama Alat Fungsi Jenis
Shell and tube heat exchanger Tube Side Fluida Butana Laju alir fluida 8382,991 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 302 (F) 880505,026 253,492 77,189
Shell Side Steam
Fluida Laju alir fluida 693,486 (lb/jam) Temperatur masuk 464 (F) Temperatur keluar 464 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
27,891 42,535 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 10 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,0825 diameter, de
Corrected 0,012 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
1 0,675 26 16
Allowab le
Calculat ed
3
0,001
Pressure Drop, ∆P (psi)
13 0,515 1,25 4 Allowab Calculat le ed 3
0,004
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
25 GAMBAR ALAT
T in
t out
T out
t in
Gambar 3.2 2-4 Heat Exchanger (kern,1965)
Tabel 3.3 Spesifikasi Heater 3 SPESIFIKASI ALAT Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
26 Nama Alat
Heater Kode Alat H-02 Memanaskan LPG Butana dan Udara Sebelum Masuk Reaktor
Fungsi Jenis
Shell and tube heat exchanger Tube Side Fluida Udara + Butana Laju alir fluida 1137995,142 (lb/jam) Temperatur masuk 566,6 (F) Temperatur keluar 734 (F) 50353256,61 365,741 1122,598
Shell Side Steam
Fluida Laju alir fluida 32604,315 (lb/jam) Temperatur masuk 1022 (F) Temperatur keluar 1022 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
95,739 122,639 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 27 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,083 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,002
Allowab le
Calculat ed
3
2,158
Pressure Drop, ∆P (psi)
1 0,810 268 16 13 0,515
1,25 4 Allowab Calculat le ed 3
0,047
GAMBAR ALAT Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
27
T in
t out
T out
t in
Gambar 3.3 2-4 Heat Exchanger (kern,1965)
Tabel 3.4 Spesifikasi Cooler 1A & 1B SPESIFIKASI ALAT Nama Alat Cooler Kode Alat
C-01A & 01B
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
28 Fungsi
Mendinginkan Produk Reaktor Sebelum Masuk Absorber
Jenis
Shell and tube heat exchanger Tube Side Fluida MA dan Udara Laju alir fluida 568997,5709 (lb/jam) Temperatur masuk 464 (F) Temperatur keluar 230 (F) 33286357,9 198,334 427,258
Shell Side Air Pendingin
Fluida Laju alir fluida 264177,4436 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 203 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
89,797 384,834 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 27 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,375 Equivalent 0,123 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,01
Allowab le
Calculat ed
10
7,987
Pressure Drop, ∆P (psi)
1,5 1,31 102 16 13 1,350
1,875 4 Allowab Calculat le ed 10
0,116
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
29
T in
t out
T out
t in
Gambar 3.4 2-4 Heat Exchanger (kern,1965)
Tabel 3.5 Spesifikasi Cooler 2 SPESIFIKASI ALAT Nama Alat Cooler Kode Alat C-02 Fungsi Mendinginkan Suhu Dibutil Ftalat Sebelum Masuk Absorber Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
30 Jenis
Shell and tube heat exchanger Tube Side Fluida Dibutil Ftalat Laju alir fluida 17400,559 (lb/jam) Temperatur masuk 325 (F) Temperatur keluar 86 (F) 1877769,358 51,068 213,574
Shell Side Air Pendingin
Fluida Laju alir fluida 20864,10397 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 167 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
167,405 168,721 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 15,25 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,083 diameter, de
Corrected 0,000 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
1 0,810 68 16
Allowab le
Calculat ed
10
0,531
Pressure Drop, ∆P (psi)
13 0,515 1,25 4 Allowab Calculat le ed 10
0,004
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
31 T in
t out
T out
t in
Gambar 3.5 2-4 Heat Exchanger (kern,1965)
Tabel 3.6 Spesifikasi Cooler 3 SPESIFIKASI ALAT Nama Alat Cooler Kode Alat C-03 Fungsi Menurunkan Suhu Maleic Anhydride Sebelum Masuk Tangki Jenis
Shell and tube heat exchanger
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
32 Shell Side Air Pendingin
Tube Side Dibutil Ftalat
Fluida Laju alir fluida 5217,252 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 167 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Fluida Laju alir fluida 6960,215 (lb/jam) Temperatur masuk 339,8 (F) Temperatur keluar 176 (F) 469552,7335 129,641 62,816 40,975 56,356 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 8 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,007
Allowab le
Calculat ed
10
0,023
Pressure Drop, ∆P (psi)
0,75 0,56 20 16 13 0,247
1 4 Allowab Calculat le ed 10
0,004
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
33 T in
t out
T out
t in
Gambar 3.6 2-4 Heat Exchanger (kern,1965)
Tabel 3.7 Spesifikasi Heat Exchanger 1A & 1B SPESIFIKASI ALAT Nama Alat Heat Exchanger Kode Alat HE-01A & 01B Menukar Panas Umpan Reaktor dengan Produk Keluaran Fungsi Reaktor Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
34 Jenis
Shell and tube heat exchanger Tube Side Fluida Udara + Butana Laju alir fluida 568998,1222 (lb/jam) Temperatur masuk 287,6 (K) Temperatur keluar 555,8 (K) 36681599,58 177,498 1004,800
Shell Side Udara + MA
Fluida Laju alir fluida 568997,5709 (lb/jam) Temperatur masuk 734 (K) Temperatur keluar 464 (K) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
27,221 205,672 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 33 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,375 Equivalent 0,123 diameter, de
Corrected 0,032 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
1,5 1,31 160 16
Allowab le
Calculat ed
10
4,267
Pressure Drop, ∆P (psi)
13 1,35 1,875 6 Allowab Calculat le ed 10
0,001
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
35 T in
t out
T out
t in
Gambar 3.7 2-6 Heat Exchanger (kern,1965)
Tabel 3.8 Spesifikasi Heat Exchanger 2 SPESIFIKASI ALAT Nama Alat Heat Exchanger Kode Alat HE-02 Fungsi Pertukaran Panas Umpan Distilasi dan Keluaran Reboiler Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
36 Jenis Shell Side Dbutil Ftalat + MA
Fluida Laju alir fluida 24360,4872 (lb/jam) Temperatur masuk 203 (F) Temperatur keluar 441,05 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Shell and tube heat exchanger Tube Side Fluida Dibutil Ftalat Laju alir fluida 17400,559 (lb/jam) Temperatur masuk 637,89 (F) Temperatur keluar 364,1 (F) 2632752,346 141,081 364,333 25,570 46,098 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 15,25 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Corrected 0,02 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
0,75 0,56 116 16
Allowab le
Calculat ed
10
1,543
Pressure Drop, ∆P (psi)
13 0,247 1 4 Allowab Calculat le ed 10
0,0016
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
37 T in
t out
T out
t in
Gambar 3.8 2-4 Heat Exchanger (kern,1965)
Tabel 3.9 Spesifikasi Condensor 1 SPESIFIKASI ALAT Nama Alat Condensor Kode Alat CD-01 Fungsi Merubah Fasa dan Mendinginkan Produk Top Distilasi 1 Jenis
Shell and tube heat exchanger
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
38 Shell Side Maleic Anhydride
Tube Side Air Pendingin
Fluida Laju alir fluida 6960,303 (lb/jam) Temperatur masuk 402,47 (F) Temperatur keluar 339,8 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Fluida Laju alir fluida 5914,986 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 158 (F) 479113,8491 43,63 113,069 123,297 15,975 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 10 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,0054
Allowab le
Calculat ed
10
9,073
Pressure Drop, ∆P (psi)
0,75 0,56 36 16 13 0,247
1 4 Allowab Calculat le ed 10
2,053
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
39 T in
t out
T out
t in
Gambar 3.9 2-4 Heat Exchanger (kern,1965)
Tabel 3.10 Spesifikasi Reboiler 1 SPESIFIKASI ALAT Nama Alat Heat Exchanger Kode Alat RB-01 Fungsi Merubah Fasa Maleic Anhydride pada Kolom Distilasi Jenis
Shell and tube heat exchanger
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
40 Shell Side Dbutil Ftalat + MA
Fluida Laju alir fluida 24360,4872 (lb/jam) Temperatur masuk 440,6 (F) Temperatur keluar 636,98 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Tube Side Steam
Fluida Laju alir fluida 4498,894 (lb/jam) Temperatur masuk 734 (F) Temperatur keluar 734 (F) 3758376,636 177,658 163,3216 32,968 129,529 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 12 Baffle Space, B (in) 4 Passes 1 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,022
Allowab le
Calculat ed
10
neg
Pressure Drop, ∆P (psi)
0,75 0,56 52 16 13 0,247
1 2 Allowab Calculat le ed 10
neg
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
41 t out
T in
t in
T out
Gambar 3.10 1-2 Heat Exchanger (Reboiler) (kern,1965)
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
Shell and tube heat exchanger Tube Side Fluida Udara Laju alir fluida 564806,6267 (lb/jam) Temperatur masuk 87,8 (F) Temperatur keluar 177,8 (F) 12708149,1 329,521 940,620
Shell Side Fluida Steam Laju alir fluida 10008,94 (lb/jam) Temperatur masuk 464 (F) Temperatur keluar 464 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF)
8,550 40,738 Allowable 0,02
Dirt factor, RD (hr)(ft2)(oF)/Btu Shell Side Shell ID (in) 25 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,0825 diameter, de
Corrected 0,0092 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft)
1 0,810 226 16
BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
H-01A & 1B
Allowab le
Calculat ed
3
0,218
Pressure Drop, ∆P (psi)
13 0,515 1,25 6 Allowab Calculat le ed 3
0,37
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
23
GAMBAR ALAT
T in
t out
T out
t in
Gambar 3.1 2-6 Heat Exchanger (kern,1965)
Tabel 3.2 Spesifikasi Heater 2 Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
24 SPESIFIKASI ALAT Heater Kode Alat H-02 Memanaskan LPG Butana Sebelum Masuk Reaktor
Nama Alat Fungsi Jenis
Shell and tube heat exchanger Tube Side Fluida Butana Laju alir fluida 8382,991 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 302 (F) 880505,026 253,492 77,189
Shell Side Steam
Fluida Laju alir fluida 693,486 (lb/jam) Temperatur masuk 464 (F) Temperatur keluar 464 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
27,891 42,535 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 10 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,0825 diameter, de
Corrected 0,012 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
1 0,675 26 16
Allowab le
Calculat ed
3
0,001
Pressure Drop, ∆P (psi)
13 0,515 1,25 4 Allowab Calculat le ed 3
0,004
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
25 GAMBAR ALAT
T in
t out
T out
t in
Gambar 3.2 2-4 Heat Exchanger (kern,1965)
Tabel 3.3 Spesifikasi Heater 3 SPESIFIKASI ALAT Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
26 Nama Alat
Heater Kode Alat H-02 Memanaskan LPG Butana dan Udara Sebelum Masuk Reaktor
Fungsi Jenis
Shell and tube heat exchanger Tube Side Fluida Udara + Butana Laju alir fluida 1137995,142 (lb/jam) Temperatur masuk 566,6 (F) Temperatur keluar 734 (F) 50353256,61 365,741 1122,598
Shell Side Steam
Fluida Laju alir fluida 32604,315 (lb/jam) Temperatur masuk 1022 (F) Temperatur keluar 1022 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
95,739 122,639 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 27 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,083 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,002
Allowab le
Calculat ed
3
2,158
Pressure Drop, ∆P (psi)
1 0,810 268 16 13 0,515
1,25 4 Allowab Calculat le ed 3
0,047
GAMBAR ALAT Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
27
T in
t out
T out
t in
Gambar 3.3 2-4 Heat Exchanger (kern,1965)
Tabel 3.4 Spesifikasi Cooler 1A & 1B SPESIFIKASI ALAT Nama Alat Cooler Kode Alat
C-01A & 01B
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
28 Fungsi
Mendinginkan Produk Reaktor Sebelum Masuk Absorber
Jenis
Shell and tube heat exchanger Tube Side Fluida MA dan Udara Laju alir fluida 568997,5709 (lb/jam) Temperatur masuk 464 (F) Temperatur keluar 230 (F) 33286357,9 198,334 427,258
Shell Side Air Pendingin
Fluida Laju alir fluida 264177,4436 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 203 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
89,797 384,834 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 27 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,375 Equivalent 0,123 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,01
Allowab le
Calculat ed
10
7,987
Pressure Drop, ∆P (psi)
1,5 1,31 102 16 13 1,350
1,875 4 Allowab Calculat le ed 10
0,116
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
29
T in
t out
T out
t in
Gambar 3.4 2-4 Heat Exchanger (kern,1965)
Tabel 3.5 Spesifikasi Cooler 2 SPESIFIKASI ALAT Nama Alat Cooler Kode Alat C-02 Fungsi Mendinginkan Suhu Dibutil Ftalat Sebelum Masuk Absorber Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
30 Jenis
Shell and tube heat exchanger Tube Side Fluida Dibutil Ftalat Laju alir fluida 17400,559 (lb/jam) Temperatur masuk 325 (F) Temperatur keluar 86 (F) 1877769,358 51,068 213,574
Shell Side Air Pendingin
Fluida Laju alir fluida 20864,10397 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 167 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
167,405 168,721 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 15,25 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,083 diameter, de
Corrected 0,000 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
1 0,810 68 16
Allowab le
Calculat ed
10
0,531
Pressure Drop, ∆P (psi)
13 0,515 1,25 4 Allowab Calculat le ed 10
0,004
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
31 T in
t out
T out
t in
Gambar 3.5 2-4 Heat Exchanger (kern,1965)
Tabel 3.6 Spesifikasi Cooler 3 SPESIFIKASI ALAT Nama Alat Cooler Kode Alat C-03 Fungsi Menurunkan Suhu Maleic Anhydride Sebelum Masuk Tangki Jenis
Shell and tube heat exchanger
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
32 Shell Side Air Pendingin
Tube Side Dibutil Ftalat
Fluida Laju alir fluida 5217,252 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 167 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Fluida Laju alir fluida 6960,215 (lb/jam) Temperatur masuk 339,8 (F) Temperatur keluar 176 (F) 469552,7335 129,641 62,816 40,975 56,356 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 8 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,007
Allowab le
Calculat ed
10
0,023
Pressure Drop, ∆P (psi)
0,75 0,56 20 16 13 0,247
1 4 Allowab Calculat le ed 10
0,004
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
33 T in
t out
T out
t in
Gambar 3.6 2-4 Heat Exchanger (kern,1965)
Tabel 3.7 Spesifikasi Heat Exchanger 1A & 1B SPESIFIKASI ALAT Nama Alat Heat Exchanger Kode Alat HE-01A & 01B Menukar Panas Umpan Reaktor dengan Produk Keluaran Fungsi Reaktor Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
34 Jenis
Shell and tube heat exchanger Tube Side Fluida Udara + Butana Laju alir fluida 568998,1222 (lb/jam) Temperatur masuk 287,6 (K) Temperatur keluar 555,8 (K) 36681599,58 177,498 1004,800
Shell Side Udara + MA
Fluida Laju alir fluida 568997,5709 (lb/jam) Temperatur masuk 734 (K) Temperatur keluar 464 (K) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
27,221 205,672 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 33 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,375 Equivalent 0,123 diameter, de
Corrected 0,032 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
1,5 1,31 160 16
Allowab le
Calculat ed
10
4,267
Pressure Drop, ∆P (psi)
13 1,35 1,875 6 Allowab Calculat le ed 10
0,001
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
35 T in
t out
T out
t in
Gambar 3.7 2-6 Heat Exchanger (kern,1965)
Tabel 3.8 Spesifikasi Heat Exchanger 2 SPESIFIKASI ALAT Nama Alat Heat Exchanger Kode Alat HE-02 Fungsi Pertukaran Panas Umpan Distilasi dan Keluaran Reboiler Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
36 Jenis Shell Side Dbutil Ftalat + MA
Fluida Laju alir fluida 24360,4872 (lb/jam) Temperatur masuk 203 (F) Temperatur keluar 441,05 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Shell and tube heat exchanger Tube Side Fluida Dibutil Ftalat Laju alir fluida 17400,559 (lb/jam) Temperatur masuk 637,89 (F) Temperatur keluar 364,1 (F) 2632752,346 141,081 364,333 25,570 46,098 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 15,25 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Corrected 0,02 Tube Side
Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
0,75 0,56 116 16
Allowab le
Calculat ed
10
1,543
Pressure Drop, ∆P (psi)
13 0,247 1 4 Allowab Calculat le ed 10
0,0016
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
37 T in
t out
T out
t in
Gambar 3.8 2-4 Heat Exchanger (kern,1965)
Tabel 3.9 Spesifikasi Condensor 1 SPESIFIKASI ALAT Nama Alat Condensor Kode Alat CD-01 Fungsi Merubah Fasa dan Mendinginkan Produk Top Distilasi 1 Jenis
Shell and tube heat exchanger
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
38 Shell Side Maleic Anhydride
Tube Side Air Pendingin
Fluida Laju alir fluida 6960,303 (lb/jam) Temperatur masuk 402,47 (F) Temperatur keluar 339,8 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Fluida Laju alir fluida 5914,986 (lb/jam) Temperatur masuk 77 (F) Temperatur keluar 158 (F) 479113,8491 43,63 113,069 123,297 15,975 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 10 Baffle Space, B (in) 4 Passes 2 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,0054
Allowab le
Calculat ed
10
9,073
Pressure Drop, ∆P (psi)
0,75 0,56 36 16 13 0,247
1 4 Allowab Calculat le ed 10
2,053
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
39 T in
t out
T out
t in
Gambar 3.9 2-4 Heat Exchanger (kern,1965)
Tabel 3.10 Spesifikasi Reboiler 1 SPESIFIKASI ALAT Nama Alat Heat Exchanger Kode Alat RB-01 Fungsi Merubah Fasa Maleic Anhydride pada Kolom Distilasi Jenis
Shell and tube heat exchanger
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
40 Shell Side Dbutil Ftalat + MA
Fluida Laju alir fluida 24360,4872 (lb/jam) Temperatur masuk 440,6 (F) Temperatur keluar 636,98 (F) Kalor umpan, Qumpan (BTU/hr) ∆T LMTD Koreksi (oF) Luas perpindahan panas (A), ft2 Clean overall coefficient, Uc (Btu/(hr)(ft2)(oF) Design overall coefficient, UD (Btu/(hr)(ft2)(oF) 2
Tube Side Steam
Fluida Laju alir fluida 4498,894 (lb/jam) Temperatur masuk 734 (F) Temperatur keluar 734 (F) 3758376,636 177,658 163,3216 32,968 129,529 Allowable 0,02
o
Dirt factor, RD (hr)(ft )( F)/Btu Shell Side Shell ID (in) 12 Baffle Space, B (in) 4 Passes 1 Clearance, C’ (in) 0,25 Equivalent 0,079 diameter, de
Tube Side Tube OD (in) Tube ID (in) Number of tube, Nt Tube length, L (ft) BWG Flow area /tube, a’ (in) Pitch (square) Passes
Pressure Drop, ∆P (psi)
Corrected 0,022
Allowab le
Calculat ed
10
neg
Pressure Drop, ∆P (psi)
0,75 0,56 52 16 13 0,247
1 2 Allowab Calculat le ed 10
neg
GAMBAR ALAT
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
41 t out
T in
t in
T out
Gambar 3.10 1-2 Heat Exchanger (Reboiler) (kern,1965)
Pra-Rancangan Pabrik Maleic Anhydride dari Butana Kel. VII/S. Genap/2018 Oleh
Diperiksa
1. Jufri Suanto Sitinjak
1. Jufri Suanto Sitinjak 2. Lamria Eufransia 3. Samuel Nainggolan
2. Lamria Eufransia 3. Samuel Nainggolan
Disetujui
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