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Biodiesel Process Version 1.01
Contents
Tab
BD
GR and MR
MB
EB
Authors: Tapasvi, Wiesenborn, Gustafson, North Dakota State University
Questions: send e-mail to [email protected]
DISCLAIMER:
Biodiesel Process Version 1.01
Mass balances, input user-selected inputs, oil composition
Energy balances
Authors: Tapasvi, Wiesenborn, Gustafson, North Dakota State University
Questions: send e-mail to [email protected]
Block diagram showing symbols of key units and stream numbering associated with crude oil pretreatment, transesterification, ester washing and drying.
Block diagram showing symbols of key units and stream numbering associated with glycerol recovery and methanol recovery.
The model is based upon published literature and common process engineering assumptions. Every effort has been made to accurately model the biodiesel process. However, this model is intended only as a demonstration of the biodiesel process modeling concept, and has not been fully and systematically tested or checked for errors. Neither the authors nor NDSU will be liable for any damages or loss of profits that may result from use of this biodiesel process model.
Mixing tank (B)
Centrifuge (C)
Crude oil (1)
Mixing tankOutstream (5)
Degummed Oil (9)
Biodiesel Production
Gums-water mix (6)
Heater (A)
Soft water (4)
Gums/Water Separation (D)
NaOH solution (9.5 wt%) (10)
Refining tank (RT)
(E)
Wash (soft) water (11)
Centrifuge (F)
Centrifugeoutstream (14)
Soapstock (13)
Phosphoric acid (3)
Gums (7)
Water (8)
Heatedcrude oil (2)
RTOutstream (12)
CSTR 1 at 60 C (J)
Methanol (20)
Sodium methoxide catalyst (19)
CSTR 1 Outstream (21)
(Methyl esters + glycerol + catalyst + excess methanol)
Separator 1 (Decanter) (K)
Glycerol + methanol + catalyst
CSTR 2 at 60 C (L)
Ester phase (23) Surge tank
(I)Centrifugeoutstream (14)
(10% solution in methanol)
Glycerol phase 1 (22)
Vacuum Oil dryer (H) 35 mm Hg absolute pressure
Water vapor (16)
Hot oil (17)
Refinedoil (18)
Heater (G)
HeaterOutstream (15)
Glycerol + methanol + catalyst
CSTR 2 at 60 C (L)
Methanol (25)
Separator 2 (Decanter) (M)
WashColumns (P)
Wash water (30)
Sodium methoxide catalyst (24)
Washed Esters (33)
Heater (O) Wash water (31)
Waste stream (32)
Ester phase (28)
Glycerol phase 2 (27)
Settler tank (Q)
Ester (35)
Aqueous phase (34)
Collecting tank (T)
Glycerol refining section
Glycerol/Aqueous phase (39)
CSTR 2 Outstream (26)
(Methyl esters + glycerol + catalyst + excess methanol)
Heater (R)
Heater (N)
HeaterOutstream (29)
Glycerol refining section
Methyl esters (Biodiesel) (38)
Vacuumester dryer
(S) 35mm Hgabsolute
pressure
Water vapor (37)
HeaterOutstream (36)
Collecting tank (T)
Heater (U)
Glycerol-alcohol stripper (V)
Glycerine hold tank (Y)
Acidulation Reactor (AR) (Z)
80% glycerine solution (51)
Methanol recoverydistillation column (W)
Decanter(AA)
Glycerol Refining and Methanol Recovery section
Condenser (X)
Glycerol/Aqueous phase (39)
Heater outstream (40)
Methanol saturated vapors + saturated steam (42)
Glycerine (47)
Hot Glycerine solution (46)
Methanol vapors (43)
Super heated steam (41)
Acidulation Reactor (AR) (Z)
80% glycerine solution (51)
Bottoms (44)
Decanter(AA)
Waste (50)(FFA/Unreacted oil)
To transesterification reactors (45)
Glycerol Refining and Methanol Recovery section
Condenser (X)
HCL(48)
AR outstream (49)
11/15/2004 GROSS MASS BALANCE: BIODIESEL PRODUCTION PROCESS(All flows are in Kilograms per day)
Input transesterification efficiency 98
Input the amount of crude oil (Kg/sec) 100
Input methanol/triglyceride ratio 6
Stream 1 2Descr. Crude Heater
Oil Outstream
Component
Water (w)Methanol (mt)Sodium Methoxide (sm)Crude Oil TG (t) 96.000 96.000 FFA (f) 0.800 0.800 Phosphatides (p) 2.000 2.000 Others (Unsaponifiable matter) (o) 1.200 1.200Glycerol (g)Soaps (s)Methyl Ester (me)NaOH (n)Phosphoric acid (pa)HCl (h)Gums (gu)
Steam (st)NaCl (na)
Total (M) 100.000 100.000
Temperature (C) 20.0 70.0Average specific heat (Kj/Kg/C) 1.917 1.917Enthalpy (Kj/Kg) (H) 38.340 134.190Mass*Enthalpy (KW) (M*H/sec) 3834.000 13419.000Phase Liquid Liquid
Fatty acid composition of oils
Fatty acid C 16 C 16:1Triglyceride Molecular weight (gm) 807.339 801.288
Composition of the oil(% age) 11 0Soybean Oil 11 0Canola Oil 4 0.5Molecular weight fraction 88.807 0.000
Molecular weight of the oil 872.869
Components of crude oilSoybean Oil Canola Oil
Triglyceride 96.000 97.250Free fatty acids 0.800 0.500Phosphatides 2.000 1.250Others 1.200 1.000
Molecular weightsg-mole
Molecular weight of oil 872.869Molecular weight of methanol 32.040Molecular weight of glycerol 92.100Molecular weight of methyl esters 292.296Molecular weight of sodium methoxide 54Molecular weight of water 18Molecular weight of NaOH 40Molecular weight of NaCL 58.5Molecular weight of HCL 36.5
Fatty acid C 16 C 16:1Molecular weight (g-mole) 256.4 254.4Soybean oil free fatty acid M.W. (g-mole) 10.256 1.272Canola oil free fatty acid M.W. (g-mole) 28.204 0
Soy FFA M.W (g-mole) 278.22Canola FFA M.W (g-mole) 281.733Molecular weight of the FFA (g-mole) 278.22Molecular weight of soap (g-mole) 278.242
Specific heat Kj/Kg/C
Soybean oil/ Soy biodiesel 1.917Canola Oil/Canola biodiesel 1.913Oil/Biodiesel 1.917
Methanol 2.55Glycerol 2.32Water 4.186
Reactions involved
FFA-NaOH (Alkali refining) RCOOH + NaOH
Amount of soap produced 0.7920626266983Amount of water produced 0.0512400258788Amount of sodium hydroxide consumed 0.11386672417511 (99% FFA removal)
FFA-Sodium methoxide (CSTR 1)
Amount of soap produced 0.00800063259291Amount of methanol produced in CSTR 1 0.00092128531378Amount of sodium methoxide consumed 0.00155272805693
Sodium methoxide-HCL (Acidulation reactor)
Amount of methanol produced 0.63811813333333Amount of sodium chloride produced 0.63811813333333Amount of hydrogen chloride consumed 0.72694481481482
Soap-HCL (Acidulation reactor) RCOONa + HCL
Amount of FFA produced 0.008Amount of sodium chloride produced 0.00168212206168Amount of hydrogen chloride consumed 0.00104952914959
RCOOH + NaOCH3
NaOCH3 + HCL
GROSS MASS BALANCE: BIODIESEL PRODUCTION PROCESS(All flows are in Kilograms per day)
3 4Phosphoric Soft
acid watersolution
0.015 1.500
0.085
0.100 1.500
C 18 C 18:1891.501 885.453
4 234 232 60
35.660 203.654
C 18 C 18:1284.4 282.45.688 169.44
11.376 64.952
RCOONa + H2O
0.115016893106175 (100% FFA removal)
RCOOH + NaCL
RCOONa + CH3OH
CH3OH + NaCL
GROSS MASS BALANCE: BIODIESEL PRODUCTION PROCESS
5 6 7 8 9Mixing tank Gums-water Gums Water Degummed Outstream mix Oil
1.515 1.507 1.507 0.008
96.000 0.480 0.480 95.5200.800 0.8000.000 0.0001.200 1.200
2.085 2.085 2.085
101.600 4.072 2.565 1.507 97.528
20.01.917
38.3403739.207
Liquid
C 18:2 C 18:3 C 20 C 22 C 22:1879.405 873.357 975.678 1059.828 1053.798
54 8 0 0 054 8 0 0 020 10.5 1.5 0 1.5
474.879 69.869 0.000 0.000 0.000
C 18:2 C 18:3 C 20 C 22 C 22:1280.4 278.4 312.5 340.5 338.556.08 29.232 4.6875 0 5.0775
151.416 22.272 0 0 0
(100% FFA removal)
10 11 12 13 14NaOH Wash Refining tank Waste Centrifuge
Solution water Outstream Outstream
2.334 15.000 17.393 17.306 0.087
95.520 2.000 93.5200.008 0.0080.000 0.0001.200 0.030 1.170
0.792 0.792
0.245 0.131 0.131
2.579 15.000 115.044 20.259 94.785
20.0 20.0 70.0 70.04.184 4.186 2.262 1.919
83.680 83.720 158.362 134.336215.794 1255.800 18218.573 12733.007Liquid Liquid Liquid Liquid
C 241143.996
000
0.000
C 24 M.W of 1 kg-mole368.6
0 0.2817330 0.27822
15 16 17 18 19Heater Water vapor Hot Oil Refined Oil Catalyst
Outstream recovered 2 in CSTR 1
0.087 0.0878.4170.935
93.520 93.520 93.5200.008 0.008 0.0080.000 0.000 0.0001.170 1.170 1.170
94.785 0.087 94.698 94.698 9.352
90.0 90.0 90.0 20.0 20.01.919 1.940 1.917 1.917 2.550
172.717 174.600 172.530 38.340 51.00016371.008 15.184 16338.246 3630.721 476.952
Liquid Vapor Liquid Liquid Liquid
20 21 22 23 24 25Methanol CSTR 1 Glycerol phase 1 Ester phase Catalyst Methanolin CSTR 1 Outstream in CSTR 2 in CSTR 2
12.180 11.655 6.993 4.662 1.263 1.8270.935 0.935 0.140
14.028 14.0280.000 0.0000.000 0.0001.170 1.1708.388 8.3880.008 0.001 0.007
79.858 79.858
12.180 116.042 16.317 99.725 1.403 1.827
20.0 60.0 55.0 20.0 20.02.550 2.015 1.947 2.550 2.550
51.000 120.888 107.063 51.000 51.000621.179 14028.121 10676.846 71.543 93.177Liquid Liquid Liquid Liquid Liquid
26 27 28 29 30 31CSTR 2 Glycerol phase 2 Ester phase Heater Wash water Heater
Outstream Outstream outstream
18.414 18.4146.413 3.848 2.565 2.565
0.140
0.281 0.281 0.2810.000 0.000 0.0000.000 0.000 0.0001.170 1.170 1.1701.283 1.2830.007 0.001 0.006 0.006
92.072 92.072 92.072
101.225 5.271 96.094 96.094 18.414 18.414
60.0 20.0 70.0 20.0 70.01.962 1.934 1.934 4.186 4.186
117.733 38.678 135.373 83.720 293.02011917.472 3716.711 13008.490 1541.648 5395.769
Liquid Liquid Liquid Liquid Liquid
32 33 34 35 36Waste stream Washed Aqueous phase Esters Heater
Esters Outstream
16.573 1.841 1.749 0.092 0.0922.565
0.281 0.281 0.2810.000 0.000 0.0000.000 0.000 0.0001.170 1.170 1.170
0.00692.072 92.072 92.072
19.144 95.364 1.749 93.614 93.614
60.0 951.890 1.890
113.372 179.50510613.211 16804.250
Liquid Liquid
37 38 39 40 41Water vapor Methyl esters Glycerol/Aqueous Heater Super-heated
(Biodiesel) phase Outstream Steam
0.092 18.322 18.32213.406 13.4061.075 1.075
0.2810.0000.0001.170
9.670 9.6700.008 0.008
92.072
80.266
0.092 93.522 42.482 42.482 80.266
95.0 95.0 20.0 64.5 250.01.940 1.917 3.203 3.203
184.300 182.115 64.063 206.602 2973.87016.969 17031.805 2721.493 8776.814 238700.818Vapor Liquid Liquid Liquid Vapor
42 43 44 45 46 47Methanol-Steam Methanol Bottoms Methanol Hot Glycerine
Vapors Vapors glycerineSaturated solution
18.322 18.32213.406 13.339 0.067 13.339
1.075 1.075
9.670 9.6700.008 0.008
80.266
111.994 13.339 18.389 13.339 10.754 10.754
100.08 100.082.343
3430.190 234.467279468.622 2521.414
Vapor Liquid
48 49 50 51HCL Acidulation Waste Glycerine
reactor (FFA/Unreacted Oil)outstreamoutstream
4.570 4.5700.638 0.638
0.008 0.008
9.670 9.670
0.807 0.079
0.640
5.377 15.605 0.008 10.308
Energy Balance
Steam (Kg/sec)
Energy Balance
Heat energy required (Q) (KW) (Kcal/sec)
(Saturated steam at 180 C, 150 psi pressure)(Difference between steam and condensate)
(3 mbar gauge pressure, 250 C)
Latent heat of vaporizationWater at 100.084 CMethanol at 64.5 C
Methanol Distillation Column Reboiler duty (KJ)(Adapted from NREL report) (Kcal)(53,676 Kcal per 1000 kg biodiesel produced)
Evaporation energy of the saturated steam (Kj/Kg) [hg-hl]
Available energy from the super-heated steam (Kj/Kg) [hsh-hg]
Heater (A)
4.757
9585.0002290.87
2015.00
717.43(Saturation temperature = 100.084 C)
Kj/kg2256.441008.00
21003.265019.90
M1H1 + Q = M2H2
M1H1 M2H2
Q
Retention tank (E)
6.455
13007.7713108.93
M9H9 + M10H10 + M11H11 + Q = M12H12
M9H9 M12H12
Q
M10H10
M11H11
Heater (G)
1.805
3638.002869.50
M14H14 + Q = M15H15
M14H14 M15H15
Q
CSTR 1 (J)
4.615
9299.2692222.58
M18H18 + M19H19 + M20H20 + Q = M21H21
M18H18M21H21
Q
M20H20
M19H19
CSTR 2 (L)
0.534
1075.906257.15 #VALUE!
M23H23 + M24H24 + M25H25 + Q = M26H26
M23H23M26H26
Q
M25H25
M24H24
Heater (N)
4.611
9291.7792220.79
M28H28 + Q = M29H29
M28H28M29H29
Q
M26H26
Heater (O)
1.913
3854.121921.16
M30H30 + Q = M31H31
M30H30M31H31
Q
Heater (R)
5.267
10613.2112536.62
M35H35 + Q = M36H36
M35H35 M36H36
Q
Heater (U)
3.005
6055.3221447.26
M39H39 + Q = M40H40
M39H39M40H40
Q
Glycerol-alcohol stripper (V)
80.266
43289.21810346.37
M40H40 + M41H41 (=Q) = M42H42 + M46H46
M40H40 M46H46
M42H42
M41H41
Satuated steam required (Kg)
43.386
Super-heated steam required (Kg)
80.266