IV - 1 ---------------------------------------------------------------------------------------------------
Pra Rencana Pabrik Alkyl Benzene Sulfonate
BAB IV NERACA PANAS
Satuan :
kilo kalori
Waktu Operasi : 1 jam proses
Suhu Refference : 25
C = 298,15 K
1. VAPORIZER V - 130 Komponen Masuk
kkalj Komponen Keluar kkalj
Entalpi Fresh SO
3
dr F-120 Entalpi Uap ke F-131
SO
3
555,6588 SO
3
121084,4788 H
2
SO
4
0,0277 H
2
SO
4
1,8969 H
2
O 0,1690 H
2
O 41,5669 555,8555
121127,9426 Entalpi Recycle dr F-131
Entalpi Liquid ke F-131 SO
3
559,8107 SO
3
559,8107 H
2
SO
4
0,0280 H
2
SO
4
0,0280 H
2
O 0,1773 H
2
O 0,1773 560,0160
560,0160 Q supply
126917,9864 Q loss 6345,8993
128033,8579 128033,8579
--------------------------------------------------------------------------------------------------- Pra Rencana Pabrik Alkyl Benzene Sulfonate
2. HEATER E - 142 Komponen Masuk
kkalj Komponen Keluar kkalj
Entalpi Udara dr G-140 Entalpi Udara ke D-150
O
2
9432,3077 O
2
38010,4966 N
2
58946,7553 N
2
237796,7630 H
2
O 1258,8333 H
2
O 5038,9350 69637,8963
280846,1946 Q supply
222324,5245 Q loss 11116,2262
291962,4208 291962,4208
3. REAKTOR R - 210 Komponen Masuk
kkalj Komponen Keluar kkalj
Entalpi Campuran dr D-150 Entalpi Campuran ke Q-220
SO
3
121084,4788 C
18
H
29
SO
3
H 7572,7277
H
2
SO
4
1,8969 C
36
H
58
S
2
O
5
8422,3575 O
2
38010,4966 H
2
SO
4
40,2385 N
2
237796,7630 Free Oil 45,6344
396893,6353 H
2
O 671,5188 Entalpi Alkyl benzene dr F-110
16752,4769 C
18
H
30
5691,7025 Entalpi Campuran ke D-211 H
2
SO
4
9,9470 SO
3
3527,1254 Free Oil
11,1761 O
2
38010,4966 H
2
O 15,7261 N
2
237796,7630 5728,5517
279334,3850 H reaksi
1220784,8069 Q supply
1172894,1914 Q loss 58644,7096
1575516,3784 1575516,3784
--------------------------------------------------------------------------------------------------- Pra Rencana Pabrik Alkyl Benzene Sulfonate
4. KOLOM SCRUBBER D - 211 Komponen Masuk
kkalj Komponen Keluar kkalj
Entalpi Campuran dr R-210 Entalpi Limbah gas
SO
3
3527,1254 SO
3
34,8677 O
2
38010,4966 O
2
13217,5114 N
2
237796,7630 N
2
82620,8350 279334,3850
95873,2141 Entalpi Air proses dr utilitas
Entalpi Limbah Cair H
2
O 14,8895 SO
3
40,2084 H
2
O 37,2533
77,4617 Q terserap
183398,5987 279349,2745
279349,2745
5. DIGESTER Q - 220 Komponen Masuk
kkalj Komponen Keluar kkalj
Entalpi Campuran dr R-210 Entalpi Campuran ke R-230
C
18
H
29
SO
3
H 7572,7277 C
18
H
29
SO
3
H 10331,8436
C
36
H
58
S
2
O
5
8422,3575 C
36
H
58
S
2
O
5
11489,8082 H
2
SO
4
40,2385 H
2
SO
4
54,5333 Free Oil
45,6344 Free Oil 62,1871
H
2
O 671,5188 H
2
O 907,2629 16752,4769
22845,6351 Q supply
6413,8507 Q loss 320,6925
23166,3276 23166,3276
6. HYDROLIZER R - 230
--------------------------------------------------------------------------------------------------- Pra Rencana Pabrik Alkyl Benzene Sulfonate
Komponen Masuk kkalj Komponen Keluar
kkalj
Entalpi Campuran dr Q-220 Entalpi ABS ke F-310
C
18
H
29
SO
3
H 10331,8436 C
18
H
29
SO
3
H 30995,2570
C
36
H
58
S
2
O
5
11489,8082 H
2
SO
4
54,5333 H
2
SO
4
54,5333 Free Oil 62,1871
Free Oil 62,1871 H
2
O 893,3948 H
2
O 907,2629 32005,3722
22845,6351 Entalpi Air proses dr utilitas
H
2
O 149,3208 H reaksi
42709,3422 Q terserap 33698,9259
65704,2981 65704,2981
7. COOLER E - 232 Komponen Masuk
kkalj Komponen Keluar kkalj
Entalpi ABS dr R-230 Entalpi ABS ke F-310
C
18
H
29
SO
3
H 30995,2570 C
18
H
29
SO
3
H 7792,9683
H
2
SO
4
54,5333 H
2
SO
4
13,9806 Free Oil
62,1871 Free Oil 15,6901
H
2
O 893,3948 H
2
O 231,1148 32005,3722
8053,7538 Q terserap
23951,6184 32005,3722
32005,3722
V - 1 ---------------------------------------------------------------------------------------------------
Pra Rencana Pabrik Alkyl Benzene Sulfonate
BAB V SPESIFIKASI ALAT
