08 neraca massa pabrik biofuel dari cpo
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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
Komponen ω Tc (K) Pc (bar) Tr-0.216 33.19 13.13 8.2298885
Bo = 0.0685228816B1 = 0.1389754035BPc/RTc = 0.0385041944Z = 1.0003610489Densitas = 0.0019629082 g/cm3
= 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
Komponen ω Tc (K) Pc (bar) Tr-0.216 33.19 13.13 20.221452
Bo = 0.07956432B1 = 0.1389994362BPc/RTc = 0.0495404418Z = 1.0096484454Densitas = 0.0763105814 g/cm3
= 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
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
-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)
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
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
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
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
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
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
Gas-liquid separator
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
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
3026
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
Gas-liquid separator
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
Gas-liquid separator
20
Waste water
21
Residu
AGO
16
17
25
Power plant
Furnace
15
24
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
10416
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
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
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
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