08 neraca massa pabrik biofuel dari cpo

Top-Notch Technology In Production Of Oils And Fats

Tempdeg, C Dinamic Viscosity mPas/cP

20 106.8 1.848 0.1726 890.125 77.19 1.861 0.1721 887.530 57.85 1.875 0.1717 88535 44.68 1.888 0.1712 882.540 35.41 1.902 0.1708 88045 28.68 1.916 0.1704 877.550 23.68 1.93 0.1699 875.155 19.88 1.944 0.1695 872.660 16.93 1.959 0.1691 870.265 14.61 1.973 0.1687 867.870 12.75 1.988 0.1683 865.475 11.23 2.003 0.1679 863.180 9.99 2.018 0.1675 860.785 8.955 2.034 0.1671 858.490 8.087 2.049 0.1668 856.195 7.351 2.065 0.1664 853.8

100 6.721 2.081 0.166 851.6105 6.179 2.097 0.1657 849.3110 5.709 2.113 0.1653 847.1115 5.298 2.129 0.165 844.9120 4.937 2.146 0.1646 842.7130 4.335 2.179 0.164 838.4135 4.083 2.197 0.1636 836.3140 3.857 2.214 0.1633 834.2145 3.653 2.231 0.163 832.1150 3.469 2.249 0.1627 830155 3.302 2.267 0.1624 828160 3.151 2.284 0.1621 825.9165 3.012 2.303 0.1618 823.9170 2.885 2.321 0.1615 821.9175 2.769 2.339 0.1613 819.9180 2.662 2.358 0.131 818185 2.563 2.377 0.1607 816.1190 2.471 2.396 0.1605 814.1195 2.387 2.415 0.1602 812.2200 2.308 2.434 0.16 810.4205 2.234 2.454 0.1597 808.5210 2.166 2.473 0.1595 806.7215 2.102 2.493 0.1693 804.9220 2.042 2.513 0.1591 803.1225 1.986 2.533 0.1589 801.3

TECHNICAL INFORMATION PALM OIL PROPERTIES

Heat Capacity KJ/kg-C

Conductivity W/m-C

Density kg/m3

230 1.933 2.554 0.1586 799.5240 1.836 2.595 0.1582 796.1245 1.792 2.616 0.1581 794.4250 1.751 2.637 0.1579 792.7255 1.711 2.658 0.1577 791260 1.674 2.68 0.1575 789.4275 1.572 2.745 0.157 784.6280 1.542 2.767 0.1569 783285 1.513 2.789 0.1568 781.5290 1.485 2.812 0.1566 779.9295 1.459 2.834 0.1565 778.4300 1.434 2.857 0.1564 776.9

Sumber: http://www.chempro.in/palmoilproperties.htmdiakses pada 20-12-2012 pukul 21.49

PERHITUNGAN DENSITAS CPO FUNGSI SUHU

Fungsi Densitas =Masukkan suhu = 110 CDensitas = 847.13642 kg/m3

Densitas CPO at 332 C masuk reaktor 768.215Densitas CPO at 120 C masuk degummimg 842.755

PERHITUNGAN KAPASITAS PANAS CPO FUNGSI SUHU

0,00039T2 - 0,52788T + 900,48422

0 50 100 150 200 250 300 3501.5

1.7

1.9

2.1

2.3

2.5

2.7

2.9

3.1

f(x) = 3.46788724627866E-06 x² + 0.00249448411327979 x + 1.79660385209692R² = 0.999999199308923

Suhu (C)

Kapa

sitas

pan

as (k

J/kg

)

0 50 100 150 200 250 300 350720

740

760

780

800

820

840

860

880

900

f(x) = 0.000386783257163066 x² − 0.527875736180154 x + 900.484215969681R² = 0.999999363849309

Suhu (C)

Dens

itas(

kg/m

^3)

KAPASITAS PANAS PALM OIL

Persamaan empiris =

DATA PROPERTIS SPK

3E-06x2 + 0,002x + 1,796

Paraffinic Kerosenes (Bio-SPK)June 2009

0 50 100 150 200 250 300 3501.5

1.7

1.9

2.1

2.3

2.5

2.7

2.9

3.1

f(x) = 3.46788724627866E-06 x² + 0.00249448411327979 x + 1.79660385209692R² = 0.999999199308923

Suhu (C)

Kapa

sitas

pan

as (k

J/kg

)

DATA PROPERTIS BIODIESEL

DATA FISIK BIODIESEL

Densitas biodiesel = 853.9

Densitas Hidrogen pada T = 332 C ; P = 5171 kPa

Operasi pada tekanan tinggi ( Smith Van Ness hal 102) digunakan persamaan generalized virial coeficient :B0 = 0,083 - 0,422/(Tr^1.6) B1 = 0,139 - 0,172/(Tr^4,2)BPc/RTc = B0 + ωB1Z = 1 + (BPc/RTc x Pr/Tr)rho uap = BM camp x P / (R T Z)Tr = T/TcPr = P/PcT = 332 C =P = 5171 kPa =BM = 44.01 g/mol

R = 83.14 cm3.bar/mol.K

Komponen ω Tc (K) Pc (bar) Tr-0.216 33.19 13.13 18.232901

Bo = 0.078945445B1 = 0.1389991292BPc/RTc = 0.0489216331Z = 1.0105670795Densitas = 0.0447597551 g/cm3

= 44.759755149 kg/m3

Densitas Hidrogen pada T = 0 C ; P = 101,325 kPa

Operasi pada tekanan tinggi ( Smith Van Ness hal 102) digunakan persamaan generalized virial coeficient :B0 = 0,083 - 0,422/(Tr^1.6) B1 = 0,139 - 0,172/(Tr^4,2)BPc/RTc = B0 + ωB1Z = 1 + (BPc/RTc x Pr/Tr)rho uap = BM camp x P / (R T Z)Tr = T/TcPr = P/PcT = 0 C =P = 101.325 kPa =BM = 44.01 g/molR = 83.14 cm3.bar/mol.K



= 1.9629081704 kg/m3

Densitas Hidrogen pada T = 398 C ; P = 5171 kPa

Operasi pada tekanan tinggi ( Smith Van Ness hal 102) digunakan persamaan generalized virial coeficient :B0 = 0,083 - 0,422/(Tr^1.6)

H2

H2

B1 = 0,139 - 0,172/(Tr^4,2)BPc/RTc = B0 + ωB1Z = 1 + (BPc/RTc x Pr/Tr)rho uap = BM camp x P / (R T Z)Tr = T/TcPr = P/PcT = 398 C =P = 5171 kPa =BM = 83.14 g/molR = 83.14 cm3.bar/mol.K



= 76.310581387 kg/m3

H2

Top-Notch Technology In Production Of Oils And Fats

DATA CRUIDE PALM OIL (CPO)

119.99 Komposisi CPO 99.31%86.97 Kandungan Jumlah65.37 3%50.63 Gum (phospolipid, phospotide) 0.030% 300 ppm40.24 Dirt 0.01%32.68 Moisture dan impurities 0.15%27.06 Sisa logam 0.50% 0.001522.78 Trigliserida 96.31%19.46 Impurities 0.690%16.84 2006, Crude Palm Oil Specification, 2006, Blue Diamond Trading & Investment, USA14.7313.0111.6110.43

9.45 Asam fosfat 0.00067 kg asam fosfat/kg CPO8.61 Carbon aktif 0.01200 kg karbon aktif/kg minyak CPO7.89 Sumber : Skripsi Jaelani, 2011 "Fraksinasi Metil Ester Olein Menggunakan Fractional-->metil ester palmitat7.286.74 INFORMASI TAMBAHAN :6.275.865.174.884.624.394.183.993.823.663.513.383.25 Sumber: Jurnal CPO dari Malaysia "Process Design Degumming and Bleaching of Palm Oil3.143.042.942.852.762.692.612.542.48

Kinematic Viscosity cST

Free Fatty Acid (FFA)

Kebutuhan untuk degumming

J19

Han: Asumsi sudah 85%

2.422.312.262.212.162.08 Sumber : Alexander Guzman, 2010 Hydroprocessing of crude palm oil at pilot plant scale

21.971.94

1.91.871.85

Flash point Palm Oil

Kandungan FFA Temperatur (C)5% 2601% 293

0.10% 315

Masukkan kandungan FFA =Flash point =

PERHITUNGAN VISCOSITY CPO FUNGSI SUHU

0% 1% 2% 3% 4% 5% 6%250

260

270

280

290

300

310

320

f(x) = − 1032.09211170995 x + 310.319206271436R² = 0.945672915753372

FFA

Suhu

(C)

0 50 100 150 200 250 300 3501.5

1.7

1.9

2.1

2.3

2.5

2.7

2.9

3.1

f(x) = 3.46788724627866E-06 x² + 0.00249448411327979 x + 1.79660385209692R² = 0.999999199308923

Suhu (C)

Kapa

sitas

pan

as (k

J/kg

)

0 50 100 150 200 250 300 350720

740

760

780

800

820

840

860

880

900

f(x) = 0.000386783257163066 x² − 0.527875736180154 x + 900.484215969681R² = 0.999999363849309

Suhu (C)

Dens

itas(

kg/m

^3)

0 50 100 150 200 250 300 3500

20

40

60

80

100

120

f(x) = 0.00172711816967263 x² − 0.700387807934504 x + 66.6782173469427R² = 0.693590813689714

Suhu (C)

Visc

osity

mPa

s

VISCOSITY PALM OIL

Persamaan empiris = 3E-06x2 + 0,002x + 1,796

0 50 100 150 200 250 300 3501.5

1.7

1.9

2.1

2.3

2.5

2.7

2.9

3.1

f(x) = 3.46788724627866E-06 x² + 0.00249448411327979 x + 1.79660385209692R² = 0.999999199308923

Suhu (C)

Kapa

sitas

pan

as (k

J/kg

)

0 50 100 150 200 250 300 3500

20

40

60

80

100

120

f(x) = 0.00172711816967263 x² − 0.700387807934504 x + 66.6782173469427R² = 0.693590813689714

Suhu (C)

Visc

osity

mPa

s

kg/m3

Konversi1 bar =1 kg =

1000000 cm3 =(pers 3.61 Smith Van Ness ed 6 hal 102)(pers 3.62 Smith Van Ness ed 6)(pers 3.59 Smith Van Ness ed 6)(pers 3.58 Smith Van Ness ed 6)

605.15 K51.71 bar

Pr3.93830921553694

(pers 3.61 Smith Van Ness ed 6 hal 102)(pers 3.62 Smith Van Ness ed 6)(pers 3.59 Smith Van Ness ed 6)(pers 3.58 Smith Van Ness ed 6)

273.15 K1.01325 bar

Pr0.07717060167555

1370.92505934233 nM3

(pers 3.61 Smith Van Ness ed 6 hal 102)

(pers 3.62 Smith Van Ness ed 6)(pers 3.59 Smith Van Ness ed 6)(pers 3.58 Smith Van Ness ed 6)

671.15 K51.71 bar

Pr3.93830921553694

2006, Crude Palm Oil Specification, 2006, Blue Diamond Trading & Investment, USA

kg asam fosfat/kg CPOkg karbon aktif/kg minyak CPO

Sumber : Skripsi Jaelani, 2011 "Fraksinasi Metil Ester Olein Menggunakan Fractional-->metil ester palmitatINFORMASI TAMBAHAN :

Sumber: Jurnal CPO dari Malaysia "Process Design Degumming and Bleaching of Palm Oil

Sumber : Alexander Guzman, 2010 Hydroprocessing of crude palm oil at pilot plant scale

0.03279.34

into Green Liquid Fuels, Rogelio Sotelo-Boyás, Fernando Trejo-Zárragaand Felipe de Jesús Hernández-Loyo

0% 1% 2% 3% 4% 5% 6%250

260

270

280

290

300

310

320

f(x) = − 1032.09211170995 x + 310.319206271436R² = 0.945672915753372

FFA

Suhu

(C)

0 50 100 150 200 250 300 3500

20

40

60

80

100

120

f(x) = 0.00172711816967263 x² − 0.700387807934504 x + 66.6782173469427R² = 0.693590813689714

Suhu (C)

Visc

osity

mPa

s

3E-06x2 + 0,002x + 1,796

0 50 100 150 200 250 300 3500

20

40

60

80

100

120

f(x) = 0.00172711816967263 x² − 0.700387807934504 x + 66.6782173469427R² = 0.693590813689714

Suhu (C)

Visc

osity

mPa

s

100 kPa1000 g

1 m3

into Green Liquid Fuels, Rogelio Sotelo-Boyás, Fernando Trejo-Zárraga

P V n R T

KONDISI REAKTORP = 1 atm 1 atm

= 5171 kPa 51 atmT = 0 C 273.15 K

= 332 C 605.15 KR = 0.08206 L.atm/mol.Kz = 1.000361Hidrogen = 5000 scf

141.584 m^3141,584.200 L

Bm hidrogen = 2.02 gram/molJumlah mol hidrogen = 6.3143012886 kmolMassa hidrogen = 12.754888603 kgVolume pada kondisi ( T=332; P 5171 kPa)

= 6.148223898 m^3

CPO = 1 barrel= 0.16 m^3

Densitas CPO 25 degC = 887.5 kg/m^3

Massa CPO = 142 kg

Untuk 1 kg reaksi CPOJumlah hidrogen = 0.0898231592 kg

Hidrogen CPO AKTUAL5000 scf 1 barrel

12.754888603 kg 142 kg0.08982315918 kg 1 kg89.8231591757 kg 1000 kg89.4099519842 kg 995.40 kg 30255.71

BOILLING POINTSenyawa C

-252.7-161.4

H2

C1

D29

Han: Asumsi suhu kamar

E43

Muflih: Jumlah CPO masuk reaktor setelah dikali kapasitas aktual

-88.6

-78.5-42

-11.7-0.6

PERHITUNGAN STOIKIOMETRI

Perbandingan CO2 dan H20 berdasarkan jurnal "Hydroprocessing of crude palm oil at pilot plant scale, 2010"

BM (kg/kmol) Komponen Perbandingbasis mol basis berat persen berat Persen berat utk neraca massa44 CO2 3 60 2640 0.7857142857143 10.76%18 H2O 2 40 720 0.2142857142857 2.94%

TOTAL 5 100 3360 1 13.70%

Perkiraan kebutuhan air untuk absorber0.39 ml gas/ liter water http://www.newton.dep.anl.gov/askasci/chem03/chem03761.htm

CO2 0.00 kg0 mol0 m^3

C2

CO2

C3

i-C4

C4

WAKTU TINGGAL DI BLEACHER

http://books.google.co.id/books?id=XSptqDdEIc0C&pg=PA257&lpg=PA257&dq=reaksi+degumming+asam+fosfat&source=bl&ots=aOM6eO_ZGV&sig=S1gP8qlUq3w-qqn5Vm0NTKTVKRY&hl=en&sa=X&ei=onbbULmaIImErQeqqoHQAg&redir_esc=y#v=onepage&q=reaksi%20degumming%20asam%20fosfat&f=falsePahan, Iyung, 1997, Paduan Lengkap Kelapa Sawit, Penebar Swadaya, Jakarta

FAKTOR PENGALI KAPASITAS AKTUAL 175,000.00 m^3/tahun

DENSITAS = 749.00 kg/m^3KAPASITAS PRODUKSI = 22.10 m^3/jam

= 16,549.87 kg/jam

HASIL SPK DARI BASIS 1 TON CPO = 544.48 kg/jamFAKTOR PENGALI = 30.40

Perhitungan kebutuhan Hidrogen

Hidrogen = 2,717.66 kgBM Hidrogen = 2.02 kg/kmol 26857 43455Mol hidrogen = 1345.378 kmol 28376 43455Z = 1.000361 55233 86910R = 0.08206 m3.atm/(kmol.K) 31677T = 273.15 KP = 1 atmV = n. R . T. Z

P= 30167.12 Nm3 (Hidrogen murni)= 31100.12 Nm3 (Hidrogen dengan pengotor 3 persen CH4)= 933.0036 Nm3 CH4

P = 1 atm 1 atm= 5171 kPa 51 atm

T = 0 C 273.15 K= 332 C 605.15 K

R = 0.08206 L.atm/mol.KZ = -32269337

Komponen ω Tc (K) Pc (bar) Tr Pr0.012 190.6 45.99 0.00524658972 0.021743857360296

Bo = -1877.111 B0 = 0,083 - 0,422/(Tr^1.6) B1 = -6.49E+08 B1 = 0,139 - 0,172/(Tr^4,2)BPc/RTc = -7786290 BPc/RTc = B0 + ωB1Z = -32269337 Z = 1 + (BPc/RTc x Pri/Tri) (Z sangat kecil sehingga bisa diabaikan)

n = 41.62465 kmolBM CH4 = 16.04 kg/kmolMassa CH4 = 667.6594 kg

C1

NERACA MASSA BASIS 1000 KG

PERHITUNGAN HIDROGEN SISA REAKSIHidrogen masuk reaktor = 89.40995 kg/jamHidrogen keluar reaktor = Hidrogen masuk reaktor + Minyak CPO (1000 kg)-Keluaran reaktor

= 51.58 kg/jamKomposisi keluar reaktor (basis 1 kg CPO)

1.0% 9.95 0.0096340.4% 3.98 0.003854

10.8% 107.15 0.103702 Neraca massa basis 1000 kg CPO7.0% 69.68 0.0674372.0% 19.91 0.0192681.6% 15.93 0.015414

13.4% 133.38 0.129094Bio-avtur 54.7% 544.48 0.526975Bio-diesel 10.0% 99.54 0.096339H20 2.9% 29.22 0.028282TOTAL 1033.22 1.00

Perbandingan CO2 dan H20 berdasarkan jurnal "Hydroprocessing of crude palm oil at pilot plant scale, 2010"

Persen berat utk neraca massa

C1

C2

CO2

C3

i-C4

C4

Naphta (C10)

http://books.google.co.id/books?id=XSptqDdEIc0C&pg=PA257&lpg=PA257&dq=reaksi+degumming+asam+fosfat&source=bl&ots=aOM6eO_ZGV&sig=S1gP8qlUq3w-qqn5Vm0NTKTVKRY&hl=en&sa=X&ei=onbbULmaIImErQeqqoHQAg&redir_esc=y#v=onepage&q=reaksi%20degumming%20asam%20fosfat&f=false

m^3/tahun 1 tahun = 330 hari24 jum

22.095959596

Perhitungan fraksi massa untuk simulasi HYSYS

H2 1542.01 0.04680C1 302.5571 0.00918C2 121.0228 0.00367CO2 3256.811 0.09885C3 2117.9 0.06428i-C4 605.1142 0.01837C4 484.0914 0.01469Naphta (C5) 4054.265 0.12305Bio-avtur 16549.87 0.50231Bio-diesel 3025.571 0.09183H2O 888.2212 0.02696TOTAL 32947.44 1.000000

(Z sangat kecil sehingga bisa diabaikan)

REAKTOR PADA BED 1

REAKTOR PADA BED 2

Sumber : Russel W. Stratton, Hsin Min Wong, James L.Hileman, 2010, Life cycle greenhouse gas emissions from alternative jet fuels

NERACA MASSA AKTUAL

PERHITUNGAN HIDROGEN SISA REAKSIHidrogen masuk reaktor 2717.664

Hidrogen masuk reaktor + Minyak CPO (1000 kg)-Keluaran reaktor Hidrogen keluar reaktor Hidrogen masuk reaktor + Minyak CPO (1000 kg)-Keluaran reaktor1567.95

Komposisi keluar reaktor (basis 1 kg CPO)1.00% 302.560.40% 121.02

10.76% 3256.817.00% 2117.902.00% 605.111.60% 484.09

13.40% 4054.27Bio-avtur 54.70% 16549.87Bio-diesel 10.00% 3025.57H20 2.94% 888.22TOTAL 31405.43

C1

C2

CO2

C3

i-C4

C4

Naphta (C5)

W53

Muflih: Hidrogen juga dikali dgn faktor kapasitas aktual

V55

Muflih: Produk keluaran reaktor juga harus dikali dengan faktor pengali kapasitas aktual


Perhitungan fraksi massa untuk simulasi HYSYS

Russel W. Stratton, Hsin Min Wong, James L.Hileman, 2010, Life cycle greenhouse gas emissions from alternative jet fuels

kg/jamHidrogen masuk reaktor + Minyak CPO (1000 kg)-Keluaran reaktor

kg/jam

Hasil keluaran reaktor setelah dikali faktor kapasitas aktual

Arus Kadar 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 1689.41 51.58 0.05 51.58 51.58

9.95 0.01 9.95 9.95 0.003.98 0.00 3.98 3.98 0.00

107.15 0.10 107.15 5.36 101.7969.68 0.06 69.68 69.6819.91 0.02 19.91 19.9115.93 0.01 15.93 15.93

133.38 0.12 133.38 40.02Bio-avtur 544.48 0.50 544.48 544.48Bio-diesel 99.54 0.09 99.54 99.54

0.0300 30.00 30.00 30.00 0.0029.22 0.03 29.22 1000.00 1000.00

Impurities 0.0069 6.90 6.90 2.30 4.60Trigliserida 0.9631 963.10 963.10 963.10

Asam fosfat 0.67 0.67 0.67

H2

C1

C2

CO2

C3

i-C4

C4

Naphta (C5)

Free Fatty Acid (FFA)H2O

Degumming&bleaching

Menara distilasi 1

Power Plant

C1 s.d C4

Bio avtur

Bio diesel

Hidrogen

Asam fosfat

Bleaching earth

Filter press

Reaktor

Gas-liquid separator

Sludge

1

3

4

5 7

6

8

10

Menara distilasi 2

15

9

16

18

19

17Naphta

20

21T : 120 °C Time: 1/2 hr

T : 332 °C

T : 398 °C

P : 5171 kPag

11

T : 120 °C Time: 0,5 hr

Crude Palm Oil(CPO)2

Absorber

12

CO2

14

Air

13

Q25

Han: Terabsorpsi 90%

I34

Han: Impurities berkurang sekitar 66,67% keluar melalui sludge

Karbon aktif 12.00 12.00 12.00

TOTAL 89.41 1000.00 0.67 12.00 1012.67 995.40 17.27 1084.81 1.00 278.18 777.41 29.22 176.39 1000.00 1101.79 684.04 0.00

Satuan : kg/jam Impurities 0.0023104

H2 0.1854 CO2 0.3852 Total 171.03

H2 0.30161C3 0.4074

O42

Han: CO2 diabsorb

17 18 19 20 21

93.37 40.02544.48

99.54 m^3literbarrel

93.37 0.00 40.02 544.48

Arus Kadar 1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19 20 212718 1568 1568 1568

970 970 970 0121 121 121 0

3257 3257 163 30942118 2118 2118

605 605 605484 484 484

4054 4054 1216 2838 1216Bio-avtur 16550 16550 16550 16550Bio-diesel 3026 3026 3026

0.0300 912 912 912 912888 888 1000 1000

Impurities 0.0069 210 210 210 70 140Trigliserida 0.9631 29274 29274 29274 29274Asam fosfat 20 20 20 20

H2

C1

C2

CO2

C3

i-C4

C4

Naphta (C5)

Free Fatty Acid (FFA)H2O

Menara distilasi 1

Power Plant

C1 s.d C4

Bio avtur

Bio diesel

Hidrogen

Asam fosfat

Bleaching earth

Filter press

Reaktor


Sludge

1

3

4

5

86

9

11

Menara distilasi 2

16

10

16

19

20

18Naphta

21

22

T : 120 °C Time: 1 hr

T : 332 °C

T : 398 °C

P : 5171 kPag

12

T : 120 °C Time: 0,5 hr

Crude Palm Oil(CPO)

2 Absorber

13

CO2

15

Air

14

Bleaching

Degumming

7

K22

Muflih: NM dikali faktor pengali dulu. Ketika jumlah palm oil berubah, keluaran produk reaktor blm ikut berubah soalnya beda rujukan cell nya

Q25

Han: Terabsorpsi 90%

J34


Karbon aktif 365 365 365 365TOTAL 2718 30396 20 365 30781 30781 30256 525 33641 9123 23630 888 6029 1000 4094 20792 0 2838 0 1216 16550

Satuan : kg/jam

Total input = 34498Total output = 35166

22 H2 0.1718655CO2 0.356985 Total 5866.29Impurities 0.0023103984 H2 0.267281

C3 0.361029

3026 m^3literbarrel

AD22

Han: CO2 diabsorb

Arus Kadar 1 2 3 4 5

2,717.66

667.7

Off gas

Bio-avtur

Bio-diesel

AGO

Residu

Impuritis 0.0069 209.73 209.73

CPO 0.9931 30,185.81 30,185.81

Asam fosfat 20.26 20.26

Karbon aktif 364.75

TOTAL 1.00 3,385.32 30,395.54 20.26 364.75 30,415.80

0.6900 %Satuan : kg/jam

Total input = 34,555.72 Kapasitas :Total output = 34,555.72

H2

C1

C2

CO2

C3

i-C4

C4

Naphta (C5)

H2O

C1 s.d C4 (Flare) ---Off Gas

Bioaviation fuelFracination Coloum

Biodiesel

Hydrogen

Phospat Acid

Bleaching earth

Filter press

ReactorGas-liquid separator

Sludge

1

3

4

5

86

11

1318

12

23

19

22

Naphta

14

Crude Palm Oil(CPO)

2

WaterMixer 2

Mixer 1

7

Furnace

9

Reactor 2

10


20

Waste water

21

Residu

AGO

16

17

25

Power plant

Furnace

15

24

Suplai hidrogen dari Pertamina RU 4 Dumai: (Budhi)26857.77

Produksi = 43419 Nm3/jam.trainJumlah train = 2Total produksi = 86838 Nm3/jam 687,756,960 Nm3/tahun

Konsumsi Pertamina HCU#211 = 26857.8 Nm3/jamHCU#212 = 28376.33 Nm3/jam 55234.13 Nm3/jam

Sisa = 31603.87 Nm3/jam

Kebutuhan H2 = 30167.12 Nm3/jam 238,923,565 Nm3/tahun

0.9545387

21,615.54

6 7 8 9 10 11 12 13 14 15

2,069.33 1,567.95 1,567.95 0.00 0.00

667.66 970.22 965.65 4.57 4.57

121.02 112.82 8.20 8.20

3,256.81 3,256.81 3,114.31 142.50 142.50

2,117.90 2,117.90 1,643.69 474.21 474.21

605.11 354.24 250.88 250.88

484.09 245.40 238.70 238.70

4,054.27 8.53 4,045.74 4,045.74

16,549.87 1.41 16,548.46 16,548.46

24,641.12 3,025.57 0.01 3,025.57 3,025.57

888.22 888.22 24.78 863.44

209.73 69.90 139.83 69.90

30,185.81 30,185.81 30,185.81

20.26 20.26

364.75 364.75

30,780.55 30,255.71 524.84 30,255.71 33,641.03 33,641.03 8,038.79 24,738.81 863.44 24,738.81

11,023.000 kg/jam Limbah : 524.84 kg/jam11.023 ton/tahun

Biodiesel87,302,161.081 kg/tahun

C1 s.d C4 (Flare) ---Off Gas

Bioaviation fuelFracination Coloum

Biodiesel

Hydrogen

Phospat Acid

Bleaching earth

Filter press

ReactorGas-liquid separator

Sludge

1

3

4

5

86

11

1318

12

23

19

22

Naphta

14

Crude Palm Oil(CPO)

2

WaterMixer 2

Mixer 1

7

Furnace

9

Reactor 2

10


20

Waste water

21

Residu

AGO

16

17

25

Power plant

Furnace

15

24

M23

Muflih: NM dikali faktor pengali dulu. Ketika jumlah palm oil berubah, keluaran produk reaktor blm ikut berubah soalnya beda rujukan cell nya

J37


87,302 ton/tahun

Nm3/tahun

437,454,310 Nm3/tahun250,302,650 Nm3/tahun

Nm3/tahun

0.87721

16 17 18 19 20 21 22 23 24 25

2,472.02 2,472.02

6,031.65 15,794.92 21,826.57

11,023.00

4,011.00

371.00

891.00

328.99 328.99 389.85

891.00 371.00 4,011.00 11,023.00 6,031.65 15,794.92 328.99 2,472.02 24,627.58 389.85

2938.32 31767.11 47770.6341

87302.2

AA36

Muflih: total steam masuk menara fraksinasi

S41

Han: Sesuai keluaran MD

U45

Han: Bioavtur dalam 1 tahun

Komposisi komponen gas :1568 0.202 20.21%

966 0.124 12.45%113 0.015 1.45%

3114 0.401 40.14%1644 0.212 21.19%

354 0.046 4.57%245 0.032 3.16%

TOTAL 7759

Komposisi Palm oil lb BM lbmolPalmitat 46 0.46 0.5152 256.4241 0.002009Stearic 4 0.04 0.0448 284.4772 0.000157Oleic 39 0.39 0.4368 282.4614 0.001546Linoleic 11 0.11 0.1232 280.4455 0.000439TOTAL 100 1.12 1103.808 0.004152

Komposisi Hidrogen lb BM LbmolTotal 0.024 2.02 0.011881

Perbandingan 2.861309CPO dari neraca massa 30256 kg/jam

kg kmolPalmitat 0.46 13917.63 54.27581

Stearic 0.04 1210.228 4.254219 87,302,161 Oleic 0.39 11799.73 41.77465

Linoleic 0.11 3328.128 11.86729

30255.71 112.172

H2 terkonsumsi di bed 1 320.9587 kmol 320958.7648.3367 kg/jam

Masuk Bed 2 2069.327 kg/jamH2 terkonsumsi di bed 2 501.38 kg/jam

REAKTOR PADA BED 1

H2

C1

C2

CO2

C3

i-C4

C4

REAKTOR PADA BED 2

Sumber : Russel W. Stratton, Hsin Min Wong, James L.Hileman, 2010, Life cycle greenhouse gas emissions from alternative jet fuels

BED 1Perbandingan reaktan di bed 1 : 46.66667Laju CPO 30256 kg/jamH2 terkonsumsi 648.3367 kg/jam

2,069.33BED 2Perbandingan reaktan di bed 2 : 126.5823H2 masuk bed 2 : 2069 kg/jam `H2 terkonsumsi : 501.38 kg/jam

AE61

Han: Jangan sampai salah memasukkan yaa

Russel W. Stratton, Hsin Min Wong, James L.Hileman, 2010, Life cycle greenhouse gas emissions from alternative jet fuels

Komposisi Palm Oil ΔHf (J/mol)44% Palmitic acid (16:0) -8484004% Stearic acid (18:0)

39% Oleic acid (18:1)11% Linoleic acid (18:2)

AlkanaPropane (3) -104680 -24290Hexadecane (16) -456300Octadecane (18) -505400CO2 -393509 -394359H2O -241818 -228572

PANAS REAKSI EKSOTERMISPanas Reaksi 2400 kj/kg minyak

KAPASITAS PANASBM (kg/kmol) A B

2 25.399 0.02017816.04 34.942 -0.03995730.07 28.146 0.04344744.01 27.437 0.0423144.1 28.277 0.116

58.12 6.772 0.3414758.12 20.056 0.28153

142.29 26.671 0.32324167.3 Bio-avtur(C12H23) 125.212 0.31401

Biodiesel (C17H36)Palm Oil

ΔG (J/mol)

H2

C1

C2

CO2

C3

i-C4

C4

Naphta (C10)

98 Phosporic acidBleaching earth (Cp didekati dgn tanah biasa)

Water 3.47 0.00347

PANAS REAKSI ASAM PALMITATSumber John C. Kotz, Paul M. Treichel, 2009, John Raymond Townsend, Chemistry & Chemical Reactivity, Thomson Higher Education, USAGoogle book http://books.google.co.id/books?id=jcn6sgt7RpoC&pg=PA252&lpg=PA252&dq=heat+of+formation+palmitic+acid&source=bl&ots=0BS6-YPujx&sig=lq9ULhovLOwMXZIcreYxuC5u9ZU&hl=en&sa=X&ei=PyfaUMz5BcbnrAec1IDIAQ&redir_esc=y#v=onepage&q=heat%20of%20formation%20palmitic%20acid&f=false

Densitas Asam Fosfathttp://web.fosfa.cz/en/phosphoric-acid-thermal-75-and-85/product.html?id=54

PANAS PENGUAPAN ASAM PALMITAT 48.6170.832015185068 kJ/kg 284.49

http://www.chemicalbook.com/ProductMSDSDetailCB9854033_EN.htm

TITIK DIDIH PALM OIL = 369 C

BLEACHING EARTH Bleaching earth: Cp-->http://www.engineeringtoolbox.com/specific-heat-solids-d_154.html

Densitas--> http://www.zchsiarkopol.pl/index.php?page=bleaching-earth

Sumber: Experimental Verification of Thermodynamic Properties of Jet-A Fuel

http://www.scielo.org.ar/pdf/laar/v38n1/v38n1a01.pdf

ASAM FOSFATCp = 0.45 cal/gCDensitas = 1689

Smith Van Ness

kj/kg minyak Sumber: Furimsky, E. Catalytic hydrodeoxygenation. Appl. Catal., A 2000, 199(2), 147.

Tavrg 347.65C D E T2 (K) T1 (K) Cp

-0.000038549 3.188E-08 -8.7585E-12 300 290 288.151325 kJ/kmol K0.00019184 -0.000000153 3.932E-11 300 290 359.221579 kJ/kmol K0.00018946 -1.9082E-07 5.3349E-11 300 290 525.519904 kJ/kmol K

-0.00001995 3.9968E-09 -2.9872E-13 300 290 382.847718 kJ/kmol K0.00019597 -0.0000002327 6.8669E-11 300 290 735.772445 kJ/kmol K

-0.00010271 -3.6819E-08 2.0429E-11 300 290 976.209536 kJ/kmol K-0.000013113 -9.4571E-08 3.4149E-11 300 290 995.375223 kJ/kmol K

0.00004282 -1.6639E-07 5.6036E-11 300 290 1214.80714 kJ/kmol K0.00079137 -0.0000009141 2.7568E-10 300 290 2632.4666 kJ/kmol K

300 200 1.42869098 kJ/kg.C300 200 2.29675 kJ/kg.C

Richardson, J.W.; Parks, G.S., Thermal data on organic compounds. XIX. Modern combustion data for some non-volatile compounds containing carbon, hydrogen and oxygen , J. Am. Chem. Soc., 1939, 61, 3543-3546Prosen, E.J.; Rossini, F.D., Heats of combustion and formation of the paraffin hydrocarbons at 25° C, J. Res. NBS, 1945, 263-267.

0.45 cal/gr.C 1.88 kJ/kg.C1.26 kJ/kg.K

0.00000145 392.15 303.15 4.85159326 kJ/kgK

John C. Kotz, Paul M. Treichel, 2009, John Raymond Townsend, Chemistry & Chemical Reactivity, Thomson Higher Education, USAhttp://books.google.co.id/books?id=jcn6sgt7RpoC&pg=PA252&lpg=PA252&dq=heat+of+formation+palmitic+acid&source=bl&ots=0BS6-YPujx&sig=lq9ULhovLOwMXZIcreYxuC5u9ZU&hl=en&sa=X&ei=PyfaUMz5BcbnrAec1IDIAQ&redir_esc=y#v=onepage&q=heat%20of%20formation%20palmitic%20acid&f=false

kJ/mol 48.6 kJ 1 kmol 1000 molkg/kmol mol 284.49 kg 1 kmol

diakses pada 27 Desember 2012 pukul 7.46

Bleaching earth: Cp-->http://www.engineeringtoolbox.com/specific-heat-solids-d_154.htmlhttp://www.zchsiarkopol.pl/index.php?page=bleaching-earth

Furimsky, E. Catalytic hydrodeoxygenation. Appl. Catal., A 2000, 199(2), 147.

26.8516.85

Thermal data on organic compounds. XIX. Modern combustion data for some non-volatile compounds containing carbon, hydrogen and oxygen , J. Am. Chem. Soc., 1939, 61, 3543-3546Heats of combustion and formation of the paraffin hydrocarbons at 25° C, J. Res. NBS, 1945, 263-267.

http://books.google.co.id/books?id=jcn6sgt7RpoC&pg=PA252&lpg=PA252&dq=heat+of+formation+palmitic+acid&source=bl&ots=0BS6-YPujx&sig=lq9ULhovLOwMXZIcreYxuC5u9ZU&hl=en&sa=X&ei=PyfaUMz5BcbnrAec1IDIAQ&redir_esc=y#v=onepage&q=heat%20of%20formation%20palmitic%20acid&f=false

J. Am. Chem. Soc., 1939, 61, 3543-3546

http://books.google.co.id/books?id=jcn6sgt7RpoC&pg=PA252&lpg=PA252&dq=heat+of+formation+palmitic+acid&source=bl&ots=0BS6-YPujx&sig=lq9ULhovLOwMXZIcreYxuC5u9ZU&hl=en&sa=X&ei=PyfaUMz5BcbnrAec1IDIAQ&redir_esc=y#v=onepage&q=heat%20of%20formation%20palmitic%20acid&f=false

cal 1 kJgram 239 calorie

10-12.11

1.0550561

1000 gram1 kg

E T Tau Cp298 330 1.107383 7430.94

100 90 1.80404137.778 49.888

kJ 2.20462 lb 1.804041 FBtu 1 kg C

C1 s.d C4 (Flare)

Bioaviation fuelFracination

Power Plant

Biodiesel

Hydrogen

Phospat Acid

Bleaching earth

Filtration

Hydrotreating

Separation

Sludge

NaphtaCrude Palm Oil

(CPO)

WaterBleaching

Degumming

Hydrocracking

405 ton/jam 3,207,600

Senyawa1 2 3 4 5 6 7 8 9 10 11 12 13 14 15 16 17 18 19

kg/jam2,717.66 - - - - - - - - 2,069.33 1,567.95 1,567.95 0.00 - - - - - -667.66 - - - - - - - - - 970.22 965.65 4.57 - - - - - -

- - - - - - - - - - 121.02 112.82 8.20 - - - - - -- - - - - - - - - 3,256.81 3,256.81 3,114.31 142.50 - - - - - -- - - - - - - - - 2,117.90 2,117.90 1,643.69 474.21 - - - - - -- - - - - - - - - - 605.11 354.24 250.88 - - - - - -- - - - - - - - - - 484.09 245.40 238.70 - - - - - -

Off gas - - - - - - - - - - - - - - - - - - -- - - - - - - - - - 4,054.27 8.53 4,045.74 - - - - - 6,031.65

Bio-avtur - - - - - - - - - - 16,549.87 1.41 16,548.46 - - - - 11,023.00 -Bio-diesel - - - - - - - - - 25,308.77 3,025.57 0.01 3,025.57 - - - 4,011.00 - -AGO - - - - - - - - - - - - - - - 371.00 - - -Residu - - - - - - - - - - - - - - 891.00 - - - -

- - - - - - - - - 888.22 888.22 24.78 - 863.44 - - - - -Impuritis - 209.73 - - 209.73 209.73 69.90 139.83 69.90 - - - - - - - - - -CPO - 30,185.81 - - 30,185.81 30,185.81 30,185.81 - 30,185.81 - - - - - - - - - -Asam fosfat - - 20.26 - 20.26 20.26 - 20.26 - - - - - - - - - - -Karbon aktif - - - 364.75 - 364.75 - 364.75 - - - - - - - - - - -TOTAL 3,385.32 30,395.54 20.26 364.75 30,415.80 30,780.55 30,255.71 524.84 30,255.71 33,641.03 33,641.03 8,038.79 24,738.81 863.44 891.00 371.00 4,011.00 11,023.00 6,031.65

H2

C1

C2

CO2

C3

i-C4

C4

Naphta (C5)

H2O

20 21 22 23kg/jam

- - - -- - - -- - - -- - - -- - - -- - - -- - - -- - 2,472.02 -

15,794.92 - - -- - - -- - - -- - - -

- - -- 328.99 389.85- - - -- - - -- - - -- - - -

15,794.92 328.99 2,472.02 389.85

Senyawakg/jam

1 2 3 4 5 6 7 8

2,717.66 - - - - - - -

667.66 - - - - - - -

- - - - - - - -

- - - - - - - -

- - - - - - - -

- - - - - - - -

- - - - - - - -

Off gas - - - - - - - -

- - - - - - - -

Bio-avtur - - - - - - - -

Bio-diesel - - - - - - - -

AGO - - - - - - - -

Residu - - - - - - - -

- - - - - - - -

Impuritis - 209.73 - - 209.73 209.73 69.90 139.83

CPO - 30,185.81 - - 30,185.81 30,185.81 30,185.81 -

Asam fosfat - - 20.26 - 20.26 20.26 - 20.26

Karbon aktif - - - 364.75 - 364.75 - 364.75

TOTAL 3,385.32 30,395.54 20.26 364.75 30,415.80 30,780.55 30,255.71 524.84

H2

C1

C2

CO2

C3

i-C4

C4

Naphta (C5)

H2O

kg/jam

9 10 11 12 13 14 15 16 17 18

- 2,069.33 1,567.95 1,567.95 0.00 - 0.00 - - -

- - 970.22 965.65 4.57 - 4.57 - - -

- - 121.02 112.82 8.20 - 8.20 - - -

- 3,256.81 3,256.81 3,114.31 142.50 - 142.50 - - -

- 2,117.90 2,117.90 1,643.69 474.21 - 474.21 - - -

- - 605.11 354.24 250.88 - 250.88 - - -

- - 484.09 245.40 238.70 - 238.70 - - -

- - - - - - - - -

- - 4,054.27 8.53 4,045.74 - 4,045.74 - - -

- - 16,549.87 1.41 16,548.46 - 16,548.46 - - -

- 25,308.77 3,025.57 0.01 3,025.57 - 3,025.57 - - 4,011.00

- - - - - - - - 371.00 -

- - - - - - - 891.00 - -

- 888.22 888.22 24.78 - 863.44 - - - -

69.90 - - - - - - - - -

30,185.81 - - - - - - - - -

- - - - - - - - - -

- - - - - - - - - -

30,255.71 33,641.03 33,641.03 8,038.79 24,738.81 863.44 24,738.81 891.00 371.00 4,011.00

kg/jam

19 20 21 22 23 24 25

- - - - - - -

- - - - - - -

- - - - - - -

- - - - - - -

- - - - - - -

- - - - - - -

- - - - - - -

- - - - 2,472.02 2,472.02 -

6,031.65 15,794.92 - - 21,826.57 -

11,023.00 - - - - - -

- - - - - - -

- - - - - - -

- - - - - - -

- - - 328.99 - 328.99 389.85

- - - - - - -

- - - - - - -

- - - - - - -

- - - - - - -

11,023.00 6,031.65 15,794.92 328.99 2,472.02 24,627.58 389.85

08 neraca massa pabrik biofuel dari cpo

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