Lampiran A Neraca Massa [PDF]

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LA-1



LAMPIRAN A NERACA MASSA Perhitungan Neraca Massa pada prarancangan pabrik Asam Akrilat dari Akrolein dan Oksigen adalah sebagai berikut: Basis Perhitungan



: 1 jam operasi



Satuan Operasi



: Kg/jam



Waktu Operasi



: 24 Jam



Kapasitas Produksi



: 120.000 Ton/tahun



Waktu kerja pertahun



: 330 hari



Kapasitas Produksi perjam



: 120.000



ton 1 tahun 1 hari 1000 kg × × × tahun 330 hari 24 jam 1 ton



: 15.151,51 kg/jam : 210,2624 kmol/jam Tabel A.1 Spesifikasi Bahan Baku dan Produk Komponen



Komposisi (%)



Berat Molekul (kg/kmol)



Bahan Baku 1. . Acrolein



56,06



- C3H4O 2. Oxygen -



O2



31,999



LA-2



Produk 1. Asam Akrilat -



C3H4O2



72,06



Kemurnian Bahan Baku: 1. C3H4O



: % (PT. Chandra Asri Petrochemical)



2. O2



:%



Kemurnian Produk



:%



Konversi



: 98,5%



A.



Reaktor Plug Flow (R-01) Berfungsi sebagai tempat terjadinya reaksi antara Akrolein dengan



oksigen sehingga menghasilkan Asam Akrilat yang akan dimurnikan pada proses selanjutnya.



LA-3



Gambar A.1 Reaktor (R-01) Dari Reaksi: C3H4O (g) + 1/2 O2 → C3H4O2 Kapasitas produksi perjam



= 15.151,51 kg/jam



BM C3H4O2



= 72,06 kg/kmol



Mol C3H4O2



=



Massa C2 H5 OH BM C2 H 5OH



Mol C3H4O2



=



15.151,51 kg/jam 72,06 kg/kmol



Mol C3H4O2



= 210,26242 kmol/jam



BM C3H4O



: 56,06 kg/kmol



BM 1/2 O2



: 31,999 kg/kmol



BM C3H4O2 : 72,06 kg/kmol



LA-4



Neraca Massa Komponen Alur 1 (F1) Acrolein : N C3H4O



=1x



Kapasitas produksi perjam Konversi



N C3H4O



=1x



210,2624 kmol/jam 98,5%



N C3H4O



= 213,4644 kmol/jam



Massa C3H4O



= 56,06 kg/kmol x 213,4644 kmol/jam = 11.966,81 kg/jam



Alur 2 (F2) Air: Berdasarkan prinsip Le Chateliers, untuk memindahkan posisi kesetimbangan ke arah kanan (produk) dapat dilakukan dengan menambahkan steam berlebih. Sesuai dengan penelitian yang telah dilakukan oleh (Hitzir, 2014) menyatakan bahwa penambahan steam berlebih sebanyak 60% dapat menggeser kesetimbangan ke arah kanan tersebut. N O2



=



1/2 x N C3H4O 1



N O2



=



1/2 x 210,26422 kmol/jam 1



= 105,1312 kmol/jam Massa O2



= 31,999 kg/kmol x 105,1312 kmol/jam = 3.364,096 kg/jam



Maka total laju alir F1+F2



= 11.966,81 kg/jam + 3.364,096 kg/jam



LA-5



= 15.330,906 kg/jam Alur (F3) : Reaksi yang terjadi C3H4O (g) + 1/2 O2 → C3H4O2 Maka komposisi produk keluaran reaktor (R-01) a.



C3H4O (masuk)



= 11.966,81 kg/jam = 213,4644 kmol/jam



C3H4O (bereaksi)



= 98,5% x Mol C3H4O masuk = 0,985 x 213,4644 kmol/jam = 210,2624 kmol/jam



C3H4O (sisa)



= 213,4644 kmol/jam - 210,2624 kmol/jam = 3,201966 kmol/jam



Massa C3H4O sisa



= 3,201966 kmol/jam x 56,06 kg/kmol = 179,5022 kg/jam



b.



O2 (masuk)



= 3.364,096 kg/jam = 105,1312 kmol/jam



O2 (bereaksi)



=



1 x mol C3H4O 2



= 105,1312 kmol/jam O2 (sisa)



= 105,1312 kmol/jam - 105,1312 kmol/jam = 0 kmol/jam



Massa O2 sisa



= 0 kmol/jam x 31,999 kg/kmol



LA-6



= 0 kg/jam c.



C3H4O2 (terbentuk)



=



1 x mol C3H4O 1



= 210,2624 kmol/jam Massa C3H4O2



= 72,06 kg/kmol x 210,2624 kmol/jam = 15.151,51 kg/jam



Tabel A.2 Neraca Massa Total Reaktor (R-01) Masuk (Kg/jam) Komponen



Out Heater-001 (F1)



Out Heater-002 (F2)



11.966,81



3.364,096 -



C3H4O O2 C3H4O2 Total



B. Separator



15.331



Keluar (Kg/jam) (F3) 179,5022 0 15.151,51 15.331



Sisa (Kg/jam) (F3) 3,201966



LA-7



Neraca Massa Total F7 = F8 + F9 Dari data hysys diketahui: Laju Alir F7 = 15.382,21 kg/jam Laju Alir F8 = 15.331 kg/jam



LA-8



Laju Alir F9 = 50,5748 kg/jam Input



Output



Fraksi Aliran F7



Fraksi Aliran F8



C3H4O



= 0,0149



C3H4O



= 0,0150



O2



= 0,0075



O2



= 0,0001



C3H4O2



= 0,9776



C3H4O2



= 0,9849



Fraksi Aliran F9 C3H4O



= 0,0005



O2



= 0,9991



C3H4O2



= 0,0004



Neraca Komponen Masuk: Aliran F7 = C3H4O O2



= X C3H4O. F7= 0,0149 x 15.382,21 kg/jam = 229,1949 kg/jam = X O2. F7



= 0,0074 x 15.382,21 kg/jam = 115,3666 kg/jam



C3H4O2 =X C3H4O2.F7 = 0,9777 x 15.382,21 kg/jam = 15.037,65 kg/jam



Neraca Komponen Keluar:



LA-9



Aliran F4 = C3H4O = X C3H4O F4



= 0,0150 x 15.382,21 kg/jam = 229,965 kg/jam



O2



= 0,0001 x 15.331,8493 kg/jam = 1,5331 kg/jam



= X H2O . O2



C3H4O2 = X C3H4O2 . F4 = 0,9849 x 15.331,8493 kg/jam =15.099,5 kg/jam Aliran F5 = C3H4O = X C3H4O . F5 O2



= 0,0005 x 50,5748 kg/jam = 0,025287 kg/jam



= X O2 . F5



=0,9991 x 50,5748 kg/jam



C3H4O2 = X C3H4O2. F5



= 50,52928 kg/jam



= 0,0004 x 50,5748 kg/jam = 0,02023 kg/jam



Tabel A.3 Neraca Massa Total Separator (S-01)



Komponen C3H4O O2 C3H4O2 Sub Total Total



C. Destilasi



Masuk (kg/jam) Out Reaktor (F3) 229,1949 115,3666 15.037,65 15.382,25 15.382,25



Keluar (kg/jam) Out Bottom Out Top Separator (F4) 229,965 1,5331 15.099,5 15.331 15.382,25



Separator (F5) 0,025287 50,59928 0,02023 50,5748



LA-10



Neraca Massa Total F9 = F10 + F11



LA-11



Dari data hysys diketahui: Laju Alir F9 = 15.331,85 kg/jam Laju Alir F10 = 178,87 kg/jam Laju Alir F11 = 15.152,98 kg/jam Input



Output



Fraksi Aliran F9



Fraksi Aliran F10



C3H4O



= 0,0150



C3H4O



= 0,9908



O2



= 0,0001



O2



= 0,0092



C3H4O2



= 0,9849



C3H4O2



=0



Fraksi Aliran F11 C3H4O



= 0,0001



Oxygen



=0



C3H4O2



= 0,9999



Neraca Komponen Masuk: C3H4O = X C3H4O . F6 = 0,0150 x 15.331,85 kg/jam O2



= X O2 . F6



= 0,0001 x 15.331,8493 kg/jam



= 229,97775 kg/jam = 1,533185 kg/jam



C3H4O2 =X C3H4O2.F6 = 0,9849 x 15.331,8493 kg/jam = 15.100,3390 kg/jam



LA-12



Neraca Komponen Keluar: Aliran F8 = C3H4O = X C3H4O . F8 = 0,9910 x 178,87 kg/jam = 177,2588 kg/jam O2



= X O2 . F8



= 0,0090 x 178,87 kg/jam = 1,6456 kg/jam



C3H4O2 = X C3H4O2. F8 = 0 x 178,87 kg/jam



= 0 kg/jam



Aliran F9 = C3H4O = X C3H4O. F9 = 0,0001 x 15.152,98 kg/jam O2



= X O2. F9



= 0 x 15.152,9805 kg/jam



= 1,5152 kg/jam = 0 kg/jam



C3H4O2 =X C3H4O2.F9 = 0,9999 x 15.152,9805 kg/jam = 15.151,46 kg/jam Tabel A.5 Neraca Massa Total Distilasi (D-01) Masuk (kg/jam) Out Bottom Komponen C3H4O O2 C3H4O2 Sub Total Total



D. Separator



Reboiled Absorber (F6) 229,97775 1,5531 15.100,3390 15.331,85 15.331,85



Keluar (kg/jam) Out Bottom Out Top Distilasi (F8)



Distilasi (F9)



177,2244 1,5152 1,6456 0 0 15.151,46 178,87 15.152,98 15.331,845



LA-13



Neraca Massa Total F10 = F11 + F12 Dari data hysys diketahui:



LA-14



Laju Alir F10 = 178,8844 kg/jam Laju Alir F11 = 177,919 kg/jam Laju Alir F12 = 0,9654 kg/jam Input



Output



Fraksi Aliran F10



Fraksi Aliran F11



C3H4O



= 0,9908



C3H4O



= 0,9986



O2



= 0,0092



O2



= 0,0040



C3H4O2



=0



C3H4O2



=0



Fraksi Aliran F12 C3H4O



= 0,1055



O2



= 0,8945



C3H4O2



=0



Neraca Komponen Masuk: Aliran F10 = C3H4O



= X C3H4O. F10



= 0,9908 x 178,8844 kg/jam = 177,2837 kg/jam



O2



= X O2 . F10



= 0,0092 x 178,8687 kg/jam = 1,6457 kg/jam



C3H4O2 = X C3H4O2. F10 = 0 x 178,8687 kg/jam



= 0 kg/jam



Neraca Komponen Keluar: Aliran F11 = Aliran F11 = C3H4O = X C3H4O F11



= 0,9986 x 177,919 kg/jam = 177,6699 kg/jam



LA-15



O2



= X O2 . F11



= 0,0090 x 177,919



kg/jam = 0,2490 kg/jam



C3H4O2 = X C3H4O2. F11 = 0 x 177,919 kg/jam



= 0 kg/jam



Aliran F5 = C3H4O = X C3H4O . F5 = 0,1055 x 0,9654 kg/jam = 0,10185 kg/jam O2



= X O2. F5



=0,8945 x 0,9654 kg/jam



= 0 kg/jam



C3H4O2 = X C3H4O2. F5 = 0 x 178,8688 kg/jam



= 0 kg/jam



Tabel A.3 Neraca Massa Total Separator (S-01)



Komponen C3H4O O2 C3H4O2 Sub Total Total



Masuk (kg/jam) Out Reaktor (F3) 177,2387 1,6457 0 178,88 178,88



Keluar (kg/jam) Out Bottom Out Top Separator (F4) 177,6699 0,2490 0 177,919 178,88



Separator (F5) 0,10185 0,86355 0 0,9654