Design Biodiesel

8/13/2019 Design Biodiesel

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Biodiesel

Contents

Tab

BD

GR and MR

MB

EB

Authors: Tapas

Questions: sen

DISCLAIMER:


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rocess Version 1.0

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 andmethanol recovery.

Mass balances, input user-selected inputs, oil composition

Energy balances

vi, Wiesenborn, Gustafson, North Dakota State University

d e-mail to [email protected]

The model is based upon published literature and common process engineering assumptions. Every effort hasbeen made to accurately model the biodiesel process. However, this model is intended only as a demonstrationof 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 thisbiodiesel process model.


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Mixing tank

(B)

Centrifuge(C)rude oil

(1)

Mixing tankOutstream (5)

DegummedOil (9)

Biod iese l Produc t ion

Gums-water mix (6)

Heater(A)

Soft water (4)

Gums/WaterSeparation (D)

NaOH solution (9.5 wt%) (10)

Refiningtank (RT)

(E)

Wash (soft) water (11)

Centrifuge(F)

Centrifugeoutstream (1

Soapstock (13)

Phosphoric acid (3)

Gums (7)

Water (8)

Heatedcrude oil

(2)

RTOutstream

(12)


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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)

Surge tank(I))

(10% solution in methanol)

Glycerol

VacuumOil dryer

(H)35 mm Hgabsolutepressure

Water vapor (16)

Hot oil(17)

Refinedoil (18)

Heater(G)

HeaterOutstream

(15)


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Glycerol + methanol + catalyst

CSTR 2 at 60 C (L)

Methanol (25)

Separator 2(Decanter)

(M)

er phase (23) WashColumns

(P)

Wash water (30)

Sodium methoxide catalyst (24)

WashedEsters (33)

Heater(O)

Wash water (31)

Waste stream (32)

ase 1 (22)

Ester phase(28)

Glycerol phase 2 (27)

Collectingtank

(T)

Glycerol refining sectionGlycerol/Aqueous phase (39)

CSTR 2 Outstream (26)

(Methyl esters +glycerol + catalyst +excess methanol)

Heater(N)

HeaterOutstream

(29)


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Methyl esters(Biodiesel)

(38)

Vacuumester dryer

(S)35mm Hgabsolutepressure

Settlertank(Q)

Ester (35)

Aqueous phase (34)

Water vapor (37)

Heater(R)

HeaterOutstream

(36)


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Collecting

tank(T)

Heater(U)

Glycerol-alcoholstripper

(V)

Glycerine hold tank

(Y)

Acidulatio(Z

80% gl

Methanol recoverydistillation column

(W)

B

Glycerol Ref in ing and Methanol Reco very se

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)


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n Reactor (AR))

ycerine solution (51)

ottoms (44)

ecanter(AA)

Waste (50)(FFA/Unreacted oil)

To transesterification reactors (45)

c t i on

Condenser(X)

HCL(48)

AR outstream (49)


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11/15/2004 GROSS MASS BALA(All flo

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) 97.250 97.250 FFA (f) 0.500 0.500 Phosphatides (p) 1.250 1.250 Others (Unsaponifiable matter) (o) 1.000 1.000Glycerol (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) 1.913 1.913Enthalpy (Kj/Kg) (H) 38.260 133.910Mass*Enthalpy (KW) (M*H/sec) 3826.000 13391.000Phase Liquid Liquid

Fatty acid composition of oils

Fatty acid C 16 C 16:1Triglyceride Molecular weight (gm) 807.339 801.288Composition of the oil(% age) 11 0Soybean Oil 4 0.5Canola Oil 11 0Molecular weight fraction 88.807 0.000


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FFA-Sodium methoxide (CSTR 1) RCOOH + NaOCH 3

Amount of soap produced 0.00500039 Amount of methanol produced in CSTR 1 0.000568623 Amount of sodium methoxide consumed 0.000958354

Sodium methoxide-HCL (Acidulation reactor) NaOCH 3 + HCL

Amount of methanol produced 0.651722154 Amount of sodium chloride produced 0.651722154 Amount of hydrogen chloride consumed 0.742442529

Soap-HCL (Acidulation reactor) RCOONa + HCL

Amount of FFA produced 0.005 Amount of sodium chloride produced 0.001038217 Amount of hydrogen chloride consumed 0.000647776


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CE: BIODIESEL PRODUCTION PR s are in Kilograms per day)

3 4Phosphoric Soft

acid water solution

0.015 0.938

0.085

0.100 0.938

C 18 C 18:1891.501 885.453

4 232 604 23

35.660 203.654


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C 18 C 18:1284.4 282.45.688 169.44

11.376 64.952

RCOONa + H 2O

0.070989199 (100% FFA re


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RCOONa + CH 3OH

CH 3OH + NaCL

RCOOH + NaCL


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CESS

5 6 7 8 9Mixing tank Gums-water Gums Water DegummedOutstream mix Oil

0.953 0.948 0.948 0.005

97.250 0.486 0.486 96.7640.500 0.5000.000 0.0001.000 1.000

1.335 1.335 1.335

101.038 2.769 1.821 0.948 98.269

20.01.913

38.2603759.753

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 0 020 10.5 1.5 0 1.554 8 0 0 0

474.879 69.869 0.000 0.000 0.000


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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

oval)


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10 11 12 13 14NaOH Wash Refining tank Waste Centrifuge

Solution water Outstream Outstream

1.440 15.000 16.477 16.394 0.082

96.764 1.250 95.5140.005 0.0050.000 0.0001.000 0.019 0.981

0.495 0.495

0.151 0.081 0.081

1.592 15.000 114.822 18.239 96.582

20.0 20.0 70.0 70.04.184 4.186 2.240 1.915

83.680 83.720 156.834 134.046133.189 1255.800 18007.941 12946.455

Liquid Liquid Liquid Liquid

C 241143.996

000

0.000


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C 24 M.W of 1 kg-mole368.6

0 0.2817330 0.27822


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15 16 17 18 19Heater Water vapor Hot Oil Refined Oil Catalyst

Outstream recovered 2 in CSTR 1

0.082 0.0828.5960.955

95.514 95.514 95.5140.005 0.005 0.0050.000 0.000 0.0000.981 0.981 0.981

96.582 0.082 96.500 96.500 9.551

90.0 90.0 90.0 20.0 20.01.915 1.940 1.913 1.913 2.550

172.344 174.600 172.170 38.260 51.00016645.442 14.384 16614.405 3692.090 487.120

Liquid Vapor Liquid Liquid Liquid


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20 21 22 23 24 25Methanol CSTR 1 Glycerol phase 1 Ester phase Catalyst Methanolin CSTR 1 Outstream in CSTR 2 in CSTR 2

12.440 11.978 7.187 4.791 1.289 1.8660.955 0.955 0.143

14.327 14.3270.000 0.0000.000 0.0000.981 0.9818.566 8.5660.005 0.001 0.005

81.561 81.561

12.440 118.373 16.709 101.665 1.433 1.866

20.0 60.0 55.0 20.0 20.02.550 2.012 1.943 2.550 2.550

51.000 120.723 106.866 51.000 51.000634.422 14290.401 10864.505 73.068 95.163

Liquid Liquid Liquid Liquid Liquid


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26 27 28 29 30 31CSTR 2 Glycerol phase 2 Ester phase Heater Wash water Heater

Outstream Outstream outstream

18.807 18.8076.579 3.948 2.632 2.632

0.143

0.287 0.287 0.2870.000 0.000 0.0000.000 0.000 0.0000.981 0.981 0.9811.310 1.3100.005 0.000 0.004 0.004

94.035 94.035 94.035

103.196 5.401 97.938 97.938 18.807 18.807

60.0 20.0 70.0 20.0 70.01.959 1.930 1.930 4.186 4.186

117.527 38.602 135.108 83.720 293.02012128.322 3780.640 13232.241 1574.515 5510.802

Liquid Liquid Liquid Liquid Liquid


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32 33 34 35 36Waste stream Washed Aqueous phase Esters Heater

Esters Outstream

16.926 1.881 1.787 0.094 0.0942.632

0.287 0.287 0.2870.000 0.000 0.0000.000 0.000 0.0000.981 0.981 0.981

0.00494.035 94.035 94.035

19.562 97.183 1.787 95.396 95.396

60.0 951.890 1.890

113.389 179.53310816.905 17126.767

Liquid Liquid


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37 38 39 40 41Water vapor Methyl esters Glycerol/Aqueous Heater Super-heated

(Biodiesel) phase Outstream Steam

0.094 18.713 18.71313.766 13.7661.098 1.098

0.2870.0000.0000.981

9.876 9.8760.005 0.005

94.035

82.082

0.094 95.302 43.459 43.459 82.082

95.0 95.0 20.0 64.5 250.01.940 1.913 3.202 3.202

184.300 181.735 64.042 206.535 2973.87017.331 17319.774 2783.193 8975.798 244101.229Vapor Liquid Liquid Liquid Vapor


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42 43 44 45 46 47Methanol-Steam Methanol Bottoms Methanol Hot Glycerine

Vapors Vapors glycerineSaturated solution

18.713 18.71313.766 13.697 0.069 13.697

1.098 1.098

9.876 9.8760.005 0.005

82.082

114.561 13.697 18.782 13.697 10.980 10.980

100.08 100.082.343

3430.190 234.479285794.381 2574.557

Vapor Liquid


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48 49 50 51HCL Acidulation Waste Glycerine

reactor /Unreacted outstreamoutstream

4.666 4.6660.652 0.652

0.005 0.005

9.876 9.876

0.823 0.080

0.6535.490 15.933 0.005 10.528


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Energy Balance

Steam (Kg/sec)

Energy Balance

Heat energy required (Q) (KW) (Kcal/sec)

Evaporation energy of the saturated steam (Kj/Kg) [h g-h l](Saturated steam at 180 C, 150 psi pressure)(Difference between steam and condensate)

Available energy from the super-heated steam (Kj/Kg) [h sh -h g](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)


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Heater (A)

4.747

M1H1 + Q = M 2H2

9565.0002286.09

2015.00

717.43(Saturation temperature = 100.084 C)

Kj/kg2256.441008.00

21403.045115.45

M1H1 M2H2

Q


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Retention tank (E)

6.382

M9H9 + M 10 H10 + M 11 H11 + Q = M 12 H12

12859.1983073.42

M9H9 M12 H12

Q

M10 H10

M11 H11


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Heater (G)

1.836

M14 H14 + Q = M 15 H15

3698.987884.08

M14 H14 M15 H15

Q


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CSTR 1 (J)

4.703

M18 H18 + M 19 H19 + M 20 H20 + Q = M 21 H21

9476.7692265.00

M18 H18 M21 H21

Q

M20 H20

M19 H19


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CSTR 2 (L)

0.544

M23 H23 + M 24 H24 + M 25 H25 + Q = M 26 H26

1095.587261.85

M23 H23 M26 H26

Q

M25 H25

M24 H24


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Heater (N)

4.691

M28 H28 + Q = M 29 H29

9451.6012258.99

M28 H28 M29 H29

Q


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Heater (O)

1.953

M30 H30 + Q = M 31 H31

3936.287940.80

M30 H30 M31 H31

Q


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Heater (R)

5.368

M35 H35 + Q = M 36 H36

10816.9052585.30

M35 H35 M36 H36

Q


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Heater (U)

3.073

M39 H39 + Q = M 40 H40

6192.6051480.07

M39 H39 M40 H40

Q


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Glycerol-alcohol stripper (V)

82.082

M40 H40 + M 41 H41 (=Q) = M 42 H42 + M46 H46

44267.70910580.24

M40 H40 M46 H46

M42 H42

M41 H41


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Satuated steam required (Kg)

43.919

Super-heated steam required (Kg)

82.082


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Documents

Design Biodiesel