Episode 4: PRODUCTION OF 60, 000 MTPA OF OLEOCHEMICAL METHYL ESTER FROM RBD PALM KERNEL OIL Micro-emulsion Process of reducing the viscosity of vegetable oil by the means of solvent (methanol, ethanol as well as normal butanol).

1. SAJJAD KHUDHUR ABBAS
Chemical Engineering , Al-Muthanna University, Iraq
Oil & Gas Safety and Health Professional – OSHACADEMY
Trainer of Trainers (TOT) - Canadian Center of Human
Development
Episode 4 : PRODUCTION OF 60, 000
MTPA OF OLEOCHEMICAL METHYL
ESTER FROM RBD PALM KERNEL OIL

2. WAN ADEEBAH WAN MAHMOOD
SITI IRHITH BUSHRAH NOOR MAHADI
SAJJAD KHUDHUR ABBAS
AIMAN MOHAMMED BELAL SIDAN
PRESENTED BY:

3. 1. To produce 60,000 MTPA of methyl esters
from RBD palm kernel oil.
2. To achieve the production of methyl esters
by using homogeneous base-catalyzed
transesterification method with sodium
methoxide (NaOCH3) as catalyst.
a) OBJECTIVES

4. What is methyl ester?
Methyl Ester
4
Fatty Acid Methyl Ester
(FAME)
Biodiesel
One of the Basic Oleochemicals
(Others: Fatty acids & Fatty alcohols)
Derived from
natural Oils & Fats
Plant Oils
Animal Fats
Waste Oils
Normally produced by:
• Transesterification of triglyceride (oil)
• Esterification of free fatty acid (FFA)
b) PROCESS BACKGROUND

5. Transesterification Process
5
Methoxide
A Triglyceride (Oil)Glycerol
A Methyl Ester
𝐓𝐓𝐓𝐓 + 𝟑𝟑 𝐌𝐌𝐌𝐌𝐌𝐌𝐌𝐌 ↔ 𝟑𝟑 𝐅𝐅𝐅𝐅𝐅𝐅𝐅𝐅 + 𝐆𝐆𝐆𝐆

6. Figure 1:Geographic
breakdown of global
oleochemicals market
(Weller, 2013)
Table 1:ASEAN oleochemical producers (ADI Finechem)
2013)
c) MARKET SURVEY
- supply & demand (global)

7. Novelty of Proposed
Design
D) PROCESS FLOW DIAGRAM

8. Reference Design
Source: (Costello, 2011)

9. P-101
P-102
P-103
P-104
M-101
E-101 E-102
E-103
E-104
E-105
E-106
E-112
E-107
E-110
E-111
C-101
R-101
E-114
E-113
E-115
C-105
P-112
P-109
P-110
P-113
P-111
P-107
P-105
C-104
C-103
T-101
(CE-810)
MeOH
NaOCH3
TG
Water
T-102
(CE-1214)
T-103
(CE-1618)
M-102
R-102 R-103
C-102
C-106
M-103
V-101
P-106
E-109
E-108
P-108
T-104
(Glycerol)
To waste water
treatment
To waste water
treatment
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1.2 atm
25 °C
1.2 atm
25 °C
1.2 atm
25 °C
1.2 atm
25 °C
1 atm
42 °C
1 atm
32 °C
1 atm
60 °C
1 atm
120 °C
1 atm
60 °C
1 atm
120 °C
1 atm
160 °C
1 atm
160 °C
1 atm
120 °C
1 atm
160 °C
1 atm
129 °C
1 atm
60 °C
1.2 atm
60 °C
1.2 atm
160 °C
1 atm
50 °C
1 atm
50 °C
1.2 atm
50 °C
1 atm
130 °C
1 atm
130 °C
1 atm
130 °C
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1 atm
176 °C
0.07 atm
176 °C
1 atm
158 °C0.25 atm
158 °C
0.25 atm
226 °C
0.45 atm
226 °C
0.25 atm
198 °C
0.07 atm
237 °C
1 atm
237 °C
1 atm
25 °C
0.5 atm
185 °C
0.7 atm
236 °C0.5 atm
236 °C
0.5 atm
25 °C
0.5 atm
59 °C
1 atm
91 °C
1.2 atm
50 °C 1 atm
50 °C
R-101
1st
Transesterification
CSTR
R-102
2nd
Transesterification
CSTR
R-103
3rd
Transesterification
CSTR
C-101
1st MeOH
Evaporator
C-102
2nd MeOH
Evaporator
V-101
ME Washing
Decanter
C-103
ME Purification
Column
C-104
CE-810 Vacuum
Column
C-105
CE-1214 and
CE-1618
Splitter
C-106
GL Purification
Column
T-101
CE-810
Storage Tank
T-102
CE-1214
Storage Tank
T-103
CE-1618
Storage Tank
T-104
GL Storage
Tank
Process Flow Diagram
9
Raw material feed
Middle/Heavy-cut Separator
Transesterification CSTRs-in-series
Glycerol Purifier
Methyl ester Purifier
Storage Tanks
Light-cut Purifier
Flash tank to recycle back
the methanol
Decanter/Wash column

10. Economic Potential 1
𝐸𝐸𝐸𝐸1 = 𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅 − 𝑅𝑅𝑅𝑅𝑅𝑅 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀 𝐶𝐶𝐶𝐶𝐶𝐶𝐶𝐶
= �(0.0813 × 60,000,000)
𝑘𝑘𝑘𝑘 𝐶𝐶𝐶𝐶810
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅3.46
𝑘𝑘𝑘𝑘
+ (0.6416 × 60,000,000)
𝑘𝑘𝑘𝑘 𝐶𝐶𝐶𝐶1214
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅4.65
𝑘𝑘𝑘𝑘
+ (0.2771 × 60,000,000)
𝑘𝑘𝑘𝑘 𝐶𝐶𝐶𝐶1618
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅3.84
𝑘𝑘𝑘𝑘
+ 8,007,371.7200
𝑘𝑘𝑘𝑘 𝐺𝐺𝐺𝐺
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅1.46
𝑘𝑘𝑘𝑘
�
− �59,542,181.6900
𝑘𝑘𝑘𝑘 𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅2.95
𝑘𝑘𝑘𝑘
+ 8,357,937.3600
𝑘𝑘𝑘𝑘 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅1.08
𝑘𝑘𝑘𝑘
�
= 𝑅𝑅𝑅𝑅 86,743,504.21/𝑦𝑦𝑦𝑦
𝑃𝑃𝑃𝑃𝑃𝑃𝑃𝑃𝑃𝑃𝑃𝑃 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀 (%) =
𝐸𝐸𝐸𝐸1
𝑅𝑅𝑅𝑅𝑅𝑅 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀 𝐶𝐶𝐶𝐶𝐶𝐶𝐶𝐶𝐶𝐶
× 100 %
=
𝑅𝑅𝑅𝑅 86,743,504.21/𝑦𝑦𝑦𝑦
𝑅𝑅𝑅𝑅 184,676,008.33/𝑦𝑦𝑦𝑦
× 100 %
= 46.97 %
 60,000 MTPA production
capacity of methyl ester
products is feasible (EP1>0) at
the continuous mode of
operation.
10

11. E) Process Selection

12. POSSIBLE PROCESSES FOR ME
SYNTHESIS
• Micro-emulsion
• Pyrolysis (thermal cracking)
• Transesterification

13. 1. Micro-emulsion
Process of reducing the viscosity of vegetable oil by the means of
solvent (methanol, ethanol as well as normal butanol).
Advantages:
• Clear
• Isotropic
• thermodynamically stable mixtures of a polar phase .
Disadvantages:
• Sticky
• Heavy carbon deposits when used as fuel
• Creates problems with the engine performance

14. 2. Pyrolysis
Pyrolysis is a conversion process by the means of heating with absence
of air resulting in ME
Advantages:
• Can use any type of raw material
• Gases oils/solvents and carbonized materials are produced
• Good viscosity
Disadvantages:
• Sticky
• When ME used as:
o fuel Fuel injection system experience damage
o High amount of carbon deposition
o Inacceptable combustion values in the engine

15. 3. Transesterification
Alcoholysis of triglycerides resulting in a mixture of
mono-alkyl esters and glycerol.
Advantages:
• Better separation of byproduct
• Achieve better viscosity product
Disadvantages:
• High methanol/oil ratio

16. Transesterification
Transesterification reaction
Chemical reaction of consumption of intermediate products

17. Transesterification Catalysis
• Base catalyst
• Acid catalyst
• Enzyme catalyst

18. Transesterification Catalysis
Alternative 1:
Base catalyst
PKO +methanol  methyl ester +glycerol
Advantages:
1. High reaction rate and high catalyst activity
2. Low methanol/oil ratio
3. Mild operation condition
Disadvantages:
1. Formation of soap
2. Limited free fatty acid,FFA content for oil
3. Inhibited by water

19. Alternative 2:
Acid catalyst
PKO +methanol  methyl ester +glycerol
Advantages:
1. Unlimited free fatty acid, FFA content for oil
2. Product can be easily separated
3. High conversion
Disadvantages:
1. Long reaction time
2. High methanol/ oil ratio
3. Acid has a stronger affinity for water

20. Alternative 3:
Lipase Enzyme
PKO + methanol  methyl ester +glycerol
Advantages:
1.More stable
2.Lipase can be regenerated and reused
Disadvantages:
1.Still under development
2.Very high cost of lipase enzyme
3.Unfavorable reaction yield and reaction time

21. (Cost) (Final decision)
(Alternative 1: Base catalyzed) Cheap Selected
(Alternative 2: Acid catalyzed) Medium Eliminated
(Alternative 3: Lipase enzyme) Expansive N/A

22. Catalyst & Alcohol Selection
1. Alcohol selection
• Methanol is selected instead of ethanol and
butanol.
• Shortest chain alcohol
• Low cost
2. Catalyst selection
• Sodium methoxide is selected instead of other
catalysts.
• Higher yield obtained
• Lower soap formation

23. Heterogeneous OR Homogenous
Catalytic Process
• Homogenous catalytic process is chosen
• Heterogeneous catalytic reaction is not been
explored and developed
• Less sources regarding heterogeneous catalytic
reaction
• Unexpected reaction rate and undesired side
reaction may encounter

24. • Higher ability to convert intermediate
products.
• Higher ability for shifting the reaction toward
desired product.
• Shorter reaction time.
• Lower reaction temperature.
• Reduced alcohol and catalyst used.
• Higher yield obtained.
Why Three Reactors

25. LEVEL 2 DECISION : INPUT-OUTPUT STRUCTURE OF
PROCESS FLOW SHEET
Species Boiling Point (oC) Destination Code
RBD Palm Kernel Oil
Not pertinent (Very
high)
Recycle (if X < 95%)
Methanol 64.7 Recycle
Sodium Methoxide (30wt% in
methanol)
a 93.0 Waste
Methyl Ester
CE-810
C8:0 b 193.0
Primary product
C10:0 b 224.0
CE-1214
C12:0 b 262.0
C14:0 b 295.0
CE-1618
C16:0 b 338.0
C18:0 b 352.0
C18:1 b 349.0
C18:2 b 366.0
Glycerol 290.0 By-product
Table 1-1: Destination code for transesterification process
Source: a (Leonid Chemicals, n.d.); b (Graboski and McCormick, 1998)

26. Reactions
The main reaction:
The side reaction:

27. ECONOMIC POTENTIAL 2
𝐸𝐸𝐸𝐸2 �
𝑅𝑅𝑅𝑅
𝑦𝑦𝑦𝑦
� = 𝑀𝑀𝑀𝑀𝑀𝑀ℎ𝑦𝑦𝑦𝑦 𝐸𝐸𝐸𝐸𝐸𝐸𝐸𝐸𝐸𝐸 𝑣𝑣𝑣𝑣𝑣𝑣𝑣𝑣𝑣𝑣 + 𝐺𝐺𝐺𝐺𝑦𝑦𝑐𝑐𝑐𝑐𝑐𝑐𝑐𝑐𝑐𝑐 𝑣𝑣𝑣𝑣𝑣𝑣𝑣𝑣𝑣𝑣 − 𝑅𝑅𝑅𝑅𝑅𝑅 𝑃𝑃𝑃𝑃𝑃𝑃 𝐶𝐶𝐶𝐶𝐶𝐶𝐶𝐶 − 𝑀𝑀𝑀𝑀𝑀𝑀ℎ𝑎𝑎𝑎𝑎𝑎𝑎𝑎𝑎 𝐶𝐶𝐶𝐶𝐶𝐶𝐶𝐶
= �(0.0813 × 60,000,000)
𝑘𝑘𝑘𝑘 𝐶𝐶𝐶𝐶810
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅3.46
𝑘𝑘𝑘𝑘
+ (0.6416 × 60,000,000)
𝑘𝑘𝑘𝑘 𝐶𝐶𝐶𝐶1214
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅4.65
𝑘𝑘𝑘𝑘
+ (0.2771 × 60,000,000)
𝑘𝑘𝑘𝑘 𝐶𝐶𝐶𝐶1618
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅3.84
𝑘𝑘𝑘𝑘
+ 8,007,371.7200
𝑘𝑘𝑘𝑘 𝐺𝐺𝐺𝐺
𝑦𝑦𝑦𝑦
×
𝑅𝑅𝑅𝑅1.46
𝑘𝑘𝑘𝑘
� − 𝑚𝑚̇ 𝑇𝑇𝑇𝑇,𝐹𝐹 ×
𝑅𝑅𝑅𝑅2.95
𝑘𝑘𝑘𝑘
− 𝑚𝑚̇ 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀,𝐹𝐹 ×
𝑅𝑅𝑅𝑅1.08
𝑘𝑘𝑘𝑘
where
𝑚𝑚̇ 𝑇𝑇𝑇𝑇,𝐹𝐹
𝑘𝑘𝑘𝑘 𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅
𝑦𝑦𝑦𝑦
= 𝐹𝐹𝑇𝑇 𝑇𝑇,𝐹𝐹
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘 𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅
𝑦𝑦𝑦𝑦
×
684.8022 𝑘𝑘𝑘𝑘
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘
=
𝑃𝑃𝑀𝑀 𝑀𝑀
𝑌𝑌
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘 𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅𝑅
𝑦𝑦𝑦𝑦
×
684.8022 𝑘𝑘𝑘𝑘
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘
𝑚𝑚̇ 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀,𝐹𝐹
𝑘𝑘𝑘𝑘 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀
𝑦𝑦𝑦𝑦
= 𝐹𝐹𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀,𝐹𝐹
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀
𝑦𝑦𝑦𝑦
×
32.0419 𝑘𝑘𝑘𝑘
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘
=
3𝑃𝑃𝑀𝑀𝑀𝑀
𝑌𝑌
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘 𝑀𝑀𝑀𝑀𝑀𝑀𝑀𝑀
𝑦𝑦𝑦𝑦
×
32.0419 𝑘𝑘𝑘𝑘
𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘𝑘

28. LEVEL 3 DECISION- RECYCLE STRUCTURE OF THE
FLOWSHEET
Block Flow Fiagram of Recycle Structure
Figure 1-2: Block Flow Diagram of Level 3 Decision

29. Reactor
Kinetic data Values
k 0.013 𝑚𝑚𝑚𝑚𝑚𝑚−1
or 0.780 ℎ𝑟𝑟−1
Activation energy, Ea 254.5 cal/mol or 1064.81 J/mol
Temperature 60°C
Pressure 1 atm
MeOH:TG molar ratio 6:1
NaOCH3 by weight of TG 1 wt%
Table 1-4: Kinetic data (Rashid et al., 2014)
Species, 𝑖𝑖
Inlet,𝐹𝐹𝑖𝑖,0 𝑀𝑀𝑀𝑀𝑖𝑖 Density 𝜌𝜌𝑖𝑖 (60°C) 𝑣𝑣𝑖𝑖
Source for density
kgmol/hr kg/kgmol kg/m3 m3/hr
TG 10.8685 684.8022 891.2 8.3514 (Timms, 1985)
MeOH 59.7911 32.0419 755.5 2.5358
(Thermal-Fluids
Central, 2010)
NaOCH3
30%
solution
6.7976 54.0240 935.0 0.3928
See Appendix A.1.1
(BASF, 2007)
Total 77.46 𝒗𝒗𝟎𝟎 = 11.2800
Table 1-5: Feed information

30. For isothermal reaction,
𝐹𝐹𝑇𝑇𝑇𝑇,0
−𝑟𝑟𝑇𝑇𝑇𝑇
=
𝑣𝑣0
𝑘𝑘 1 − 𝑋𝑋
where
𝑣𝑣0 = 11.28 𝑚𝑚3
/ℎ𝑟𝑟
𝑘𝑘 60°C = 0.780 ℎ𝑟𝑟−1
For adiabatic reaction,
𝐹𝐹𝑇𝑇𝑇𝑇,0
−𝑟𝑟𝑇𝑇𝑇𝑇
=
𝑣𝑣0
𝑘𝑘 1 − 𝑋𝑋
where
𝑘𝑘 ℎ𝑟𝑟−1
= 0.780 exp
1064.81
8.314
1
333.15
−
1
𝑇𝑇
𝑇𝑇(𝐾𝐾𝐾𝐾𝐾𝐾𝐾𝐾𝐾𝐾𝐾𝐾) = −6.3376𝑋𝑋 + 333.16
0
200
400
600
800
1000
1200
1400
1600
0.0 0.2 0.4 0.6 0.8 1.0
FTG,0/(-rTG)(m3)
Conversion, X
Levenspiel Plot (Isothermal)
Figure 1-3: Levenspiel Plot (Isothermal: constant k)
0
200
400
600
800
1000
1200
1400
1600
0.0 0.2 0.4 0.6 0.8 1.0
FTG,0/(-rTG)(m3)
Conversion, X
Levenspiel Plot (Adiabatic)
Figure 1-4: Levenspiel Plot (Adiabatic: k changes with temperature)

31. 31
 99% conversion
 RM73 million/yr
Highest Profit : RM75.5 million/yr
Conversion : 82%
Optimum Profit : RM73 mil/yr
Conversion : 99%
Small Gap: RM2.5 mil/yr
ECONOMIC POTENTIAL 3

32. P-101
P-102
P-103
P-104
M-101
E-101 E-102
E-103
E-104
E-105
E-106
E-112
E-107
E-110
E-111
C-101
R-101
E-114
E-113
E-115
C-105
P-112
P-109
P-110
P-113
P-111
P-107
P-105
C-104
C-103
T-101
(CE-810)
MeOH
NaOCH3
TG
Water
T-102
(CE-1214)
T-103
(CE-1618)
M-102
R-102 R-103
C-102
C-106
M-103
V-101
P-106
E-109
E-108
P-108
T-104
(Glycerol)
To waste water
treatment
To waste water
treatment
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1.2 atm
25 °C
1.2 atm
25 °C
1.2 atm
25 °C
1.2 atm
25 °C
1 atm
42 °C
1 atm
32 °C
1 atm
60 °C
1 atm
120 °C
1 atm
60 °C
1 atm
120 °C
1 atm
160 °C
1 atm
160 °C
1 atm
120 °C
1 atm
160 °C
1 atm
129 °C
1 atm
60 °C
1.2 atm
60 °C
1.2 atm
160 °C
1 atm
50 °C
1 atm
50 °C
1.2 atm
50 °C
1 atm
130 °C
1 atm
130 °C
1 atm
130 °C
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1 atm
25 °C
1 atm
176 °C
0.07 atm
176 °C
1 atm
158 °C0.25 atm
158 °C
0.25 atm
226 °C
0.45 atm
226 °C
0.25 atm
198 °C
0.07 atm
237 °C
1 atm
237 °C
1 atm
25 °C
0.5 atm
185 °C
0.7 atm
236 °C0.5 atm
236 °C
0.5 atm
25 °C
0.5 atm
59 °C
1 atm
91 °C
1.2 atm
50 °C 1 atm
50 °C

33. M-101
M-102
E-101
R-100 E-102
C-101 C-102
M-103
E-103
E-104
V-101
E-105
E-106
C-103
E-108
C-104
E-110
C-105
C-106
E-113
P-105
P-101
P-102
P-103
P-104
P-106
P-107
P-108
E-107
P-110
E-109
P-113
E-114
E-115
E-111
E-112
P-112
P-111
P-109
2
4
3
5 6
7
MEOH
8
9 15
1011
13
14
18
22
16
20
23
25
27
28
31
33
34
37
40
42
43
45
12
1
NAOCH3
TG
WATER
17
21
24
26
32
30
41
44
46
36
39
19
35
38
29

35. Reactor
Component
Stream
6 6a 6b 7
Mass Flow (kg/hr)
TG 7,517.9522 1,611.8490 345.8258 75.1795
ME-8 29.4362 263.5800 320.0806 331.3242
ME-10 7.3485 221.3613 268.8119 278.6136
ME-12 29.0846 2,886.9164 3,505.7513 3,637.0365
ME-14 2.9385 931.7397 1,131.4660 1,174.6950
ME-16 0.4539 465.6010 565.4065 587.3475
ME-18 0.4448 1,181.3929 1,434.6344 1,490.9591
GL 0.8427 794.2666 964.5243 1,000.9215
MeOH 2,110.5902 1,281.5504 1,103.8387 1,065.8481
Water
NaOCH3 81.3248 81.3248 81.3248 81.3248
Total 9,780.4164 9,719.5819 9,721.6643 9,723.2498

36. k 0.78 hr-1
vo 11.28 m3/hr
Conv.
Number of CSTRs, n
Volume of each CSTR (m3)
x 1 2 3 4 5
0.1 2 1 1 0 0
0.4 10 4 3 2 2
0.5 14 6 4 3 2
0.7 34 12 7 5 4
0.8 58 18 10 7 5
0.9 130 31 17 11 8
0.955 307 54 26 17 12
0.99 1432 130 53 31 22

37. Component
Stream
MeOH NaOCH3 TG 3
Enthalpy Flow
kW kW kW kW
TG-8 0.00 0.00 -309.31 -309.31
TG-10 0.00 0.00 -237.91 -237.91
TG-12 0.00 0.00 -2892.25
-
2892.25
TG-14 0.00 0.00 -835.41 -835.41
TG-16 0.00 0.00 -394.70 -394.70
TG-18 0.00 0.00 -971.66 -971.66
Summarized results of streams’ enthalpy flow

38. Pump
Fluid Power
Manual Calculation Result
kW
P-101 0.008053
P-102 0.000237
P-103 0.034578
P-104 0.049475
P-105 0.007785
P-106 0.059666
P-107 0.050024
P-108 0.060870
P-109 0.016567
P-110 0.055166
P-111 0.168413
P-112 0.079416
P-113 0.054530

39. Stream
Mass Flow
Error
Theo. & Hysys
Error
Theo. &
Superpro
Manual Result Aspen Result Superpro
kg/hr kg/hr kg/hr
46 1187.1491 1231.4500 1158.579 3.60% -2.46%
30 588.4234 597.2062 608.059 1.47% 3.22%
36 4769.9296 4800.5740 4823.224 0.64% 1.1%
39 2156.0437 2171.9230 2129.760 0.73% 1.23%
Code Definition
46 Glycerol
30 ME8-10
36 ME12-14
39 ME 16-18

40. EQUIPMENT SIZING
Distillation Column Design Summary
EQUIPMENT SPECIFICATION SHEET
Equipment C-103 C-104 C-105
Material of Construction SS 304 SS 304 SS 304
Feed Trays (from top) 10 7 20
Liquid Flow Pattern Single pass Single pass Single pass
Tray spacing, lt (m) 0.6 0.6 0.6
Column diameter, Dc (m) 1.18 1.09 1.27
Column cross-sectional area, Ac (m2) 1.09 0.93 1.26
Column height, ht (m) 18.13 15.06 19.99
No. of trays 28 24 32
Provisional Plate Design
Plate thickness, tp (mm) 5 5 5
Plate area
Down comer area, Ad (m2) 0.16 0.14 0.19
Net area, An (m2) 0.93 0.79 1.07
Active area, Aa (m2) 0.76 0.65 0.88
Hole area, Ah (m2) 0.09 0.08 0.11
Hole Design
Hole diameter, dh (mm) 5 5 5
Single hole area, Ash (m2) 1.96E-05 1.96E-05 1.96E-05
Number of holes 4658 3960 5384

41. Assumptions
Optimizations
Conclusion
1. Reactors
2. Distillation column
3. Decanter
1. Operating conditions
2. Assumptions
3. Economic potential EP
4. Sizing and costing
5. Recycle
With these assumptions and
optimizations , we can produce
60,000 ton of ME per year .

42. Thanks for Watching
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