PRA RANCANGAN PABRIK PEMBUATAN BIODIESEL DARI CPO

Cooler
Air Pendingin
T = 30°C

ΔΗ9 ΔΗ 11
T = 90°C, 1 atm T = 35°C, 1 atm

Minyak jarak Minyak
Air Air
Air Pendingin Buangan, T = 50°C

Total ΔH keluar pada alur 11 = 12154,0338 kkal/jam
Panas yang diserap = > Q diserap = ΔHin – Δhout = 78667,4427 – 12154,0338
= 68877,4433 kkal/jam'

Jadi panas yang diserap oleh air pendingin pada alur keluar sebesar 68877,4433 kkal/jam'
Temperatur air pendingin keluar 50 oC = 323 K,
Maka jumlah air pendingin yang dibutuhkan
=> F air dingin = Panas diserap air dingin / Cp dt
= 68877,4433 kkal/jam' / 18,0152 kkal/mol.k ( 323-298)K
148,4911 kmol/jam x 18 kg/kmol
= 1672,84 kg/jam

Alur 4
F4 minyak = 2.991,0063 kg/jam
F4 Karbohidrat = 800,0634 kg/jam
F4 Serat = 769,2917 kg/jam
F4Protein = 1.089,3171 kg/jam
F4 H2O = 602,4007 kg/jam
F4 Abu = 141,5497 kg/jam
F4 getah = 24,6173 kg/jam
F4 IPA 85% = 1.495,5032 kg/jam

Alur 6
F6 Minyak = ( Recovery ) (2.991,0063)
= 98/ 100 ( 2.991,00632) = 2.931,1862 kg/jam

F6 IPA 85% = ( Recovery ) (1.495,5032 )
= 98/100 ( 1.465,5032)
= 1.465,5931kg/jam

F6 H2O = F4 H2O

Alur 5

F5 minyak = F4 minyak – F6 minyak
= 59,8201 kg/jam

F5 Karbohidrat = F4 Karbohidrat = 800,0634 kg/jam
F5 Serat = F4 Serat = 769,2917 kg/jam
F5 Protein = F4 Protein = 1.089,3171 kg/jam
F5 Abu = F4 Abu = 141,5497kg/jam
F5 H2O = F4 H2O - F6 H2O
= 596,3767 kg/jam

F5 getah = F4 getah = 24,6173 kg/jam
F5 IPA 85% = F4 IPA 85% - F6 IPA 85%
= 29,9101 kg/jam
FLASH VAPORIZER

F8 IPA 85 % F8
F8 Air

F7 Steam, 120oC, 1 atm
F7 Minyak
F7 Air Kondensor 1000C,1 atm
F7 IPA F9
F9 Minyak
F9Air

Persamaan neraca massa pada flash vaporizer
F7 = F8 + F9

FLASH VAPORIZER

Alur 7
F7 minyak = F6 minyak = 2.931,1862 kg/jam
F7 IPA 85% = F6 IPA 85% = 1.465,5931 kg/jam
F7 H2O = F6 H2O = 6,0240 kg/jam

Alur 8
F8 H2O = F7 H2O – F9 H2O
= 6,0240 – ( 15/100 x 6,0240)
= 5.1204 kg/jam
Alur 9
F9 IPA 85% = F6 IPA 85% = 1.465,5931 kg/jam
F9 H2O = 15/ 100 6,0240 = 0.9036 kg/jam

NERACA PANAS
Basis Perhitungan : 1 jam operasi
Suhu Referensi : 25 oC = 298 oK

Data estimasi kapasitas panas (cP) dalam kkal/kg oK (Tabel 3-336,Perry)
Cp tri miristat : 0.4851 kkal/kg K : 350.7800 kkal/kmol. oK
Cp tri palmitat : 0.4884 kkal/kg oK : 394.3400 kkal/kmol. oK
Cp tri steara t : 0.4912 kkal/kg oK : 473.9000 kkal/kmol. oK
Cp tri oleat : 0.4799 kal/kg oK : 424.9400 kkal/kmol. oK
Cp tri linoleat : 0.4685 kkal/kg oK : 411.9800 kkal/kmol. oK
Cp metil miristat : 0.4918 kkal/kg oK : 119.2200 kkal/kmol. oK
Cp metil palmitat : 0.4945 kkal/kg oK : 133.7400 kkal/kmol. oK
Cp metil stearat : 0.4967 kkal/kg oK : 148.2600 kkal/kmol. oK
Cp metil oleat : 0.4855 kkal/kg oK : 143.9400 kkal/kmol. oK
Cp metil linoleat : 0.4741 kkal/kg oK : 139.6200 kkal/kmol. oK
Cp asam miristat : 111.9653 kkal/kmol. oK
Cp asam palmitat : 123.0232 kkal/kmol. oK
Cp asam stearat : 136.4934 kkal/kmol. oK
Cp asam oleat : 137.3295 kkal/kmol. oK
Cp asam linoleat : 133.3410 kkal/kmol. oK
Cp air : 1.0000 kal/kg oK : 18.0152 kkal/kmol. oK
Cp metanol : 0.6068 kal/kg oK : 19.5000 kkal/kmol. oK
Cp gliserol : 0.5605 kal/kg oK : 51.6200 kkal/kmol. oK
Cp KOH : 0.2123 kkal/kg oK : 0.0038 kkal/kmol. oK
Cp karbohidrat : 1.88 kj/kg oK
Cp protein : 1.68 kj/kg oK
Cp abu : 0.54 kkal/kg oC : 0.0020 kkal/kg. oK
Cp getah : 0.54 kkal/kg oC : 0.0020 kkal/kmol. oK
Cp H3PO4 : 0.6468 kal/g oC : 0.2160 kkal/kmol. oK
Cp IPA : 34.6310 kkal/kmol oK
Cp ampas : (4,13.10-3 + 0.0064.10-3t) kkal/kmol. oK
Cp serat : 0.672 kal/gr oC : 0.0025 kkal/kg. oK
Cp minyak jarak : 341.8448 kkal/kmol. oK

Ball Mill (BM)

ΔH1 ΔH2
Biji jarak remah jarak
T = 30oC, 1 atm T = 30oC, 1 atm

Pada alat ini tidak terjadi perubahan panas, sehingga :

ΔHin tot = ΔHout,tot

BM

Kondensor subcooler
Air Pendingin
T = 30°C

ΔΗ8 ΔΗ 10 = 58,2650 kkal/jam
T = 90°C, 1 atm T = 40°C, 1 atm

Air Air
IPA IPA
Kondensat , T = 50°C

Total ΔH keluar pada alur 10 = 58,2650 kkal/jam
Panas yang diserap = > Q diserap = ΔHin – Δhout = 285.945,4627 – 58,2650
= 285.915, 4391 kkal/jam'

Jadi panas yang diserap oleh air pendingin pada alur keluar sebesar 285.951, 4391 kkal/jam
Temperatur air pendingin keluar 50 oC = 323 K,
Maka jumlah air pendingin yang dibutuhkan
=> F air dingin = Panas diserap air dingin / Cp dt
= 285.951,4391 kkal/jam / 18,0152 kkal/mol ( 323-298)K
= 63,9115 kmol/jam x 18 kg/kmol
= 11.428,41 kg/jam

TERIMA KASIH ……………….
Apakah Ada Pertanyaan…..?

FILTER PREES (FP)

Recovery 98 %
F4 F6

F4 Minyak F6 Minyak
F4 Karbohidrat F5 F6 Air
F4 Serat F6 IPA
F4 Air
F4 Protein
F4Abu F5 Minyak
F4 Getah F5 Karbohidrat
F4 IPA 85 % F5 Serat
F5 Air
F5 Protein
F5Abu
F5 Getah
F5 IPA 85 %

Persamaan neraca massa pada filter press

F4 = F5 + F6

FILTER PREES

Alur 2
F2 remah jarak = 6.154,3340 kg/jam
F2 minyak = 48,60/100 x 6.154,3340 = 2.991,0063 kg/jam
F2 Karbohidrat = 13.00/100 x 6.154,3340 = 800,0634 kg/jam
F2 Serat = 12.5 /100 x 6.154,3340 = 769,2917 kg/jam
F2 Protein = 17.70/100 x 6.154,3340 = 1.089,3171 kg/jam
F2 Abu = 2.30/100 x 6.154,3340 = 141,5497 kg/jam
F2 H2O = 5.50/100 x 6.154,3340 = 338,4884 kg/jam
F2 getah = 0.40/100 x 6.154,3340 = 24,6173 kg/jam

Alur 3
F3 IPA 85% = ½ x 2.991,0063 = 1.495,5032 kg/jam
= 100/85 x 1.495,5032 = 1.759,4155 kg/jam
F3 H2O = 1.759,4155 – 1.495,5032 = 263,9123 kg/jam

PRA RANCANGAN PABRIK PEMBUATAN BIODIESEL DARI BIJI JARAK KAPASITAS 21.700 TON/TAHUN

TUGAS NERACA ENERGI : IBU PRATIWI PUTRI LESTARI, S.T., M.T.
Di Susun Oleh :
Hongce Jaya
DESKRIPSI PROSES

1. Proses Ekstraksi Buah Jarak
2. Proses Pencampuran Metanol dan KOH
3. Proses Transesterifikasi
4. Proses Pemisahan
5. Proses Pencucian
6. Proses Pemurnian Metil Ester

Alur 4

F4 Karbohidrat = F2 Karbohidrat = 800,0634 kg/jam
F4 Serat = F2 Serat = 769,2917 kg/jam
F4 Protein = F2 Protein = 1.089,3171 kg/jam

F4 H2O = F2 H2O + F3 H2O
= 338,4884 + 263,9123
= 602,4007 kg/jam

F4 Abu = F2 Abu = 141,5497 kg/jam
F4 getah = F2 getah = 24,6173 kg/jam
F4IPA 85% = F3IPA 85% = 1.495,5032 kg/jam

NERACA MASSA

Kapasitas Produksi = 21,700 ton/tahun
1 Tahun Operasi = 330 hari
1 Hari Produksi = 24 jam
Kapasitas produksi dalam 1 jam operasi :
= 21700 ton 1000 kg 1 ton 1 hari
Tahun 1 ton 330 hari 24 jam

= 2.739,8990 kg/jam

Basis perhitungan : 1 jam operasi
Kemurnian produk 98 %
Biodiesel murni sebagai produk
= 98 % x 2.739,8990 kg/jam
= 2.685,1010 kg/jam

BALL MILLER (BM)

F1 Biji Jarak F2 Remah Biji Jarak

Persamaan neraca massa pada mixer (M)
F1 = F2

Komponen Massa masuk (kg/jam) Massa keluar (kg/jam)
Alur 1 Alur 2
Biji Jarak 6.154,3340 6.154,3340
Total 6.154,3340 6.154,3340

BALL MILLER

EKSTRAKTOR (EK)

F3
F3 IPA 85 %

F2 F4

F2 Minyak F4 Minyak
F2 Karbohidrat F4 IPA
F2 Serat F4 Karbohidrat
F2 Air F4 Air
F2 Protein F4 Protein
F2 Abu F4 Abu
F2 Getah F4 Getah
F4 Serat

Persamaan neraca massa pada ekstraktor (EK)
F2 + F3 = F4

EKSTRAKTOR

Komposisi Biodiesel dalam % massa : (O'Brein, 1998)
Metil Miristat = 0.10 %
Metil Palmitat = 14.70 %
Metil Stearat = 6.75 %
Metil Oleat = 40,05 %
Metil Linoleat = 36.60 %

Berat Molekul Biodiesel : (Perry, 1999)
Metil Miristat = 242,39 kg/kmol
Metil Palmitat = 270,44 kg/kmol
Metil Stearat = 298,49 kg/kmol
Metil Oleat = 296,48 kg/kmol
Metil Linoleat = 294, 44 kg/kmol

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PRA RANCANGAN PABRIK PEMBUATAN BIODIESEL DARI CPO

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