Description Glycerolysis procedure is more economical - fats are cheaper and less glycerol is required. Fats and fatty acids are insoluble in glycerol - high temperatures are required to force the reaction to proceed. On production scale, direct esterification and interesterification can be done continuously or batchwise. Generally, there will be input for the process and output from the process. Here we can define what are the related variables or input-output that present in this process. Feed stream: In this process, the feed raw material is assumed already pure, so no need to purify the feed streams. Excess reactant: fatty acid is fed as an excess reactant and is supplied in liquid form. Recycle and purge: There are recycle stream from glycerol and fatty acid but there are no purges from the process.

1. SAJJAD KHUDHUR ABBAS
Ceo , Founder & Head of SHacademy
Chemical Engineering , Al-Muthanna University, Iraq
Oil & Gas Safety and Health Professional – OSHACADEMY
Trainer of Trainers (TOT) - Canadian Center of Human
Development
Episode 75 :PRODUCTION OF
100MT DISTILLED MONOGLYCERIDE
(DMG)

3. Formed
biochemically
via release of a
fatty acid from
diacylglycerol
by
diacylglycerol
lipase.
Monoglyceride
(MG) - chemical
compound a.k.a
monoacylglycerol
Industrial
chemical and
biological
processes.
General
Information
Act as
emulsifiers - mix
ingredients that
would not
otherwise blend
well

7. • Glycerolysis procedure is more economical -
fats are cheaper and less glycerol is required.
• Fats and fatty acids are insoluble in glycerol -
high temperatures are required to force the
reaction to proceed.
• On production scale, direct esterification and
interesterification can be done continuously
or batchwise.

10. COMPONENTS Appearance Formula
MW
(g/mol)
Tb
(K)
Tf
(K)
ΔfHo
298
(kJ/mol)
GLYCEROL
- Clear
viscous
liquid
- Little or no
odor
C3H5(OH)3 92.0900 444 472 -669.60
MONOGLYCERIDES
(MONOSTEARIN)
- Colorless
- Odorless
- Sweet-taste
- Flaky
powder
C21H4204 358.5558 940.09 424.9 -1031.31
DIGLYCERIDES
(DISTEARIN)
- White to
pale
yellow
- Wax-like
solid
- Mild fatty
odour
C39H76O5 625.0177 1336.04 454.8 -1495.40

12. Proposed Process Batch Continuous
• Operating 24 hr/day
• Production is
continuous
• Total batch time 3-5 hours
• 7 batches/day production
• Operating 24 hr/day
• Production is
continuous
• 99% purity • 40 - 60% purity • 98% purity
• Annual cost is higher • Annual cost is lower • Annual cost is higher
• Lower maintenance
cost
• Higher specific
manufacturing and
operating cost
• Higher maintenance
cost

14. 𝐶3 𝐻5 𝑂𝐻 3 + 𝑅𝑂𝐶𝑂𝐻 → 𝐶3 𝐻5 𝑂𝐻 2 𝑂𝐶𝑂𝑅+ 𝐻2 𝑂
𝐶3 𝐻5 𝑂𝐻 2 𝑂𝐶𝑂𝑅+ 𝑅𝑂𝐶𝑂𝐻 → 𝐶3 𝐻5 𝑂𝐻 𝑂𝐶𝑂𝑅 2 + 𝐻2 𝑂
Reaction 1
Reaction 2
Rate constant 350oF 460oF
k1 0.291 1.566
k2 0.163 0.220

16. r1=k1CGCFA(1)
r2=k2CMCFA(2)
Base on consecutive reaction
• Glycerol
−
𝑑𝐶 𝐺
𝑑𝑡
= −𝑟𝐺 = 𝑘1 𝐶 𝐺 𝐶 𝐹𝐴 (3)
• Fatty acid
−
𝑑𝐶 𝐹𝐴
𝑑𝑡
= −𝑟𝐹𝐴 = 𝑟1 + 𝑟2 = 𝑘1 𝐶 𝐺 𝐶 𝐹𝐴 + 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴 (4)
• Monoglyceride
𝑑𝐶 𝑀
𝑑𝑡
= 𝑟 𝑀 = 𝑟1 − 𝑟2 = 𝑘1 𝐶 𝐺 𝐶 𝐹𝐴 − 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴(5)
• Water
𝑑𝐶 𝑊
𝑑𝑡
= 𝑟 𝑊 = 𝑟1 + 𝑟2 = 𝑘1 𝐶 𝐺 𝐶 𝐹𝐴 + 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴(6)
• Diglyceride
𝑑𝐶 𝐷
𝑑𝑡
= 𝑟 𝐷 = 𝑟2 = 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴(7)

17. 𝐶 𝐺 = 𝐶 𝐺𝑜 1 − 𝑋 𝐺 (8)
−
𝑑𝐶 𝐺
𝑑𝑡
=
𝑑 𝐶 𝐺𝑜 1 − 𝑋 𝐺
𝑑𝑡
= 𝐶 𝐺𝑜
𝑑𝑋 𝐺
𝑑𝑡
= 𝑘1 𝐶 𝐺𝑜 1 − 𝑋 𝐺 𝐶 𝐹𝐴
𝑑𝑋 𝐺
𝑑𝑡
= 𝑘1 1 − 𝑋 𝐺 𝐶 𝐹𝐴(9)
−
𝑑𝐶 𝐹𝐴
𝑑𝑡
= 𝑘1 𝐶 𝐺𝑜 1 − 𝑋 𝐺 𝐶 𝐹𝐴 + 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴 (10)
𝑑𝐶 𝑀
𝑑𝑡
= 𝑘1 𝐶 𝐺𝑜 1 − 𝑋 𝐺 𝐶 𝐹𝐴 − 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴 (11)
𝑑𝐶 𝑊
𝑑𝑡
= 𝑘1 𝐶 𝐺𝑜 1 − 𝑋 𝐺 𝐶 𝐹𝐴 + 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴(12)
𝑑𝐶 𝐷
𝑑𝑡
= 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴(13)

18. • By applying chain rule;
−
𝑑𝐶 𝐺
𝑑𝑋 𝐺
=
𝑘1 𝐶 𝐺𝑜 1−𝑋 𝐺 𝐶 𝐹𝐴
𝑘1 1−𝑋 𝐺 𝐶 𝐹𝐴
= 𝐶 𝐺𝑜 (14)
−
𝑑𝐶 𝐹𝐴
𝑑𝑋 𝐺
=
𝑘1 𝐶 𝐺𝑜 1−𝑋 𝐺 𝐶 𝐹𝐴+𝑘2 𝐶 𝑀 𝐶 𝐹𝐴
𝑘1 1−𝑋 𝐺 𝐶 𝐹𝐴
= 𝐶 𝐺𝑜 +
𝑘2 𝐶 𝑀
𝑘1 1−𝑋 𝐺
(15)
𝑑𝐶 𝑀
𝑑𝑋 𝐺
=
𝑘1 𝐶 𝐺𝑜 1−𝑋 𝐺 𝐶 𝐹𝐴 − 𝑘2 𝐶 𝑀 𝐶 𝐹𝐴
𝑘1 1−𝑋 𝐺 𝐶 𝐹𝐴
= 𝐶 𝐺𝑜 −
𝑘2 𝐶 𝑀
𝑘1 1−𝑋 𝐺
(16)
𝑑𝐶 𝑊
𝑑𝑋 𝐺
=
𝑘1 𝐶 𝐺𝑜 1−𝑋 𝐺 𝐶 𝐹𝐴+𝑘2 𝐶 𝑀 𝐶 𝐹𝐴
𝑘1 1−𝑋 𝐺 𝐶 𝐹𝐴
= 𝐶 𝐺𝑜 +
𝑘2 𝐶 𝑀
𝑘1 1−𝑋 𝐺
(17)
𝑑𝐶 𝐷
𝑑𝑋 𝐺
=
𝑘2 𝐶 𝑀 𝐶 𝐹𝐴
𝑘1 1−𝑋 𝐺 𝐶 𝐹𝐴
=
𝑘2 𝐶 𝑀
𝑘1 1−𝑋 𝐺
(18)

22. Generally, there will be input for the process and output from
the process. Here we can define what are the related
variables or input-output that present in this process.
Feed stream: In this process, the feed raw material is assumed
already pure, so no need to purify the feed streams.
Excess reactant: fatty acid is fed as an excess reactant and is
supplied in liquid form.
Recycle and purge: There are recycle stream from glycerol and
fatty acid but there are no purges from the process.

24. (30)
G
AM
FA
X
XP
F  (31
GM
M
W
XS
P
P  (32
 G
GM
M
G X
XS
P
R  1 (33
 A
G
M
E X
X
P
F  1 (34
M
M
FG
S
P
F 

25. 
nj
j1
N
 Hrj
m
 Picpi
i1
M
 Ta Tm   0
Energy balances
Simplified;
Where;

26. • Where from the process,

27. • 𝑇𝑎 = 𝑇 𝑚 −
𝑗−1
𝑁
𝑛 𝑗∆𝐻 𝑟𝑗
𝑚
𝑖−1
𝑀
𝑃 𝑖 𝑐 𝑝𝑖
𝑗=1
𝑁
𝑛𝑗∆𝐻𝑟𝑗
𝑚
= 𝐹𝐹𝐺 𝑆 𝑀 𝑋 𝐺 ∆𝐻𝑟1
°
+ 𝐹𝐹𝐺 𝑆 𝑀 𝑋 𝐺∆𝐻𝑟2
°
+
𝐹𝐹𝐺 𝑆 𝑀 𝑋 𝐺 𝑐 𝑝 𝑀
+ 𝐹𝐹𝐺 𝑆 𝑀 𝑋 𝐺 𝑐 𝑝 𝐷
+ 𝐹𝐹𝐺 𝑋 𝐺 𝑐 𝑝 𝑊
−𝐹𝐹𝐺 1 − 𝑋 𝐺 𝑐 𝑝 𝐺
− 𝐹𝐹𝐺 1 − 𝑋 𝐺 𝑐 𝑝 𝐹𝐴
𝑇 𝑚 − 25

28. 𝑖=1
𝑀
𝑃𝑖 𝑐 𝑝𝑖 = 𝐹𝐹𝐺 1 − 𝑋 𝐺 𝑐 𝑝𝐺 + 𝐹𝐹𝐺 1

29. XG Ta(K)
0.1
25.04766
0.2
26.71848
0.3
30.5613
0.4
38.46259
0.5
53.72134
0.6
82.52075
0.7
136.2711
0.8
230.746
0.9
367.7698
1
504.2849

31. • Isothermal heat load can be obtained from
𝑄 =
𝑗=1
𝑁
𝑛𝑗∆𝐻𝑟𝑗
𝑚
+
𝑖=1
𝑀
𝑃𝑖 𝑐 𝑝𝑖 𝑇 𝑚 − 25
𝑄
=
𝑃 𝑀
𝑆 𝑀 𝑋 𝐺
𝑆 𝑀 𝑋 𝐺 ∆𝐻𝑟1
°
+ 𝑆 𝑀 𝑋 𝐺∆𝐻𝑟2
°
+
𝑆 𝑀 𝑋 𝐺 𝑐 𝑝 𝑀
+ 𝑆 𝑀 𝑋 𝐺 𝑐 𝑝 𝐷
+ 𝑋 𝐺 𝑐 𝑝 𝑊
− 1 − 𝑋 𝐺 𝑐 𝑝 𝐺
− 1 − 𝑋 𝐺 𝑐 𝑝 𝐹𝐴
𝑇 𝑚 − 25

32. • Operation conditions:
• Reactor Temperature = 255°C
• Pressure, PT = 1.063 bar
• R = 8.3144 kJ.K/kmole
𝐶3 𝐻5 𝑂𝐻 3 + 𝑅𝑂𝐶𝑂𝐻 → 𝐶3 𝐻5 𝑂𝐻 2 𝑂𝐶𝑂𝑅 + 𝐻2 𝑂 molkJHo
r /2.1171

𝐶3 𝐻5 𝑂𝐻 2 𝑂𝐶𝑂𝑅 + 𝑅𝑂𝐶𝑂𝐻 → 𝐶3 𝐻5 𝑂𝐻 𝑂𝐶𝑂𝑅 2 + 𝐻2 𝑂 molkJHo
r /77.212


33. For CSTR;
21 rr
XF
V GG


 M
GM
M
GM
M
GG
S
XS
P
XS
P
XF
V


1
M
G
P
XF
V
2
G


35. • The annual reactor cost;

39. • Determination of Minimum Number of Stages
• Minimum and Actual Reflux Ratio
𝑁 𝑚𝑖𝑛 =
𝑙𝑜𝑔
𝑑 𝐿𝐾
𝑑 𝐻𝐾
𝑏 𝐻𝐾
𝑏 𝐿𝐾
𝑙𝑜𝑔𝛼 𝑚
𝑅 𝑚𝑖𝑛 =
𝑙𝑜𝑔
𝑥 𝐿𝐻𝑑
𝑑 𝑋𝐻𝐾𝑑
− 𝛼 𝐿𝐾,𝐻𝐾
𝑋 𝐻𝐾𝑑
𝑋 𝐿𝐾
𝛼 𝐿𝐾,𝐻𝐾
−1

40. • Theoretical and Actual Number of Stages
– The theoretical number of stages, N is calculated by using Gilliland
correlation:
• Calculated column diameter D = 4.9388 m
• Column Height = 17.0688 m
𝑵 − 𝑵 𝑴𝑰𝑵
𝑵 + 𝟏
= 𝟏 − 𝒆𝒙𝒑
𝟏 + 𝟓𝟒. 𝟒𝒙
𝟏 + 𝟏𝟏𝟕. 𝟐𝒙
𝒙 − 𝟏
𝒙

41. Calculation for Distillation Column
Component Feed Distillate Bottom
Molar flow Mol fraction Molar flow Mol fraction Molar flow Mol fraction
Distearin 13.8064 0.1648 0.0166 0.0009 13.7898 0.2092
Glycerin 20.1735 0.2408 17.8092 0.9973 2.3643 0.0359
Monostearin 36.1002 0.4309 0.0051 0.0003 36.0952 0.5476
Fatty Acid 13.6934 0.1635 0.0260 0.0015 13.6674 0.2073
Total 83.7736 1.0000 17.8568 1.0000 65.9167 1.0000

42. Fenske ( Nmin)
Parameter/Component Glycerol (LK) Monostearin (HK)
Distillate Flow Rate, di 17.81 0.01
Bottom Flow Rate,bi 2.36 36.10
(αlk,hk)N 3.190282151
(αlk,hk)1 1.979918231
Nmin 14

43. Gilliland correlation
Calculated column diameter D = 4.9388 m
Column Height = 17.0688 m
Rmin 1.75
Reflux Ratio, R 2.1
X 0.1129
Y 0.48275
N 28

44. • Where;
A = capacity or size parameter of the equipment
K1, K2, K3 = values used in the correlation
𝑙𝑜𝑔10 𝐶 𝑝
𝑜 = 𝐾1 + 𝐾2 𝑙𝑜𝑔10 𝐴 + 𝐾3[𝑙𝑜𝑔10 𝐴 ]2

45. EP4 = EP3 - 𝐶 𝑝
𝑜
(distillation column)

48. Stream Type Tsupply (K)
Ttarget
(K)
Total Heat
Capacity
Flowrate, FCp
(KW/K)
Enthalpy
Change,
∆H (KW)
H1 Hot 498.15 373.15 8.76 -1094.50
H2 Hot 498.15 328.15 2.37 -402.86
C1 Cold 298.15 328.15 0.834 25.011
C2 Cold 328.15 393.15 5.494 357.124
Total Q available = 2898.458 KW
Total Q that must be absorbed = 2898.458 KW

49. Stream Type Tsupply(K) Ttarget(K) TsS TsT ∆T ∆H FCp (KW/K)
H1 Hot 498.15 373.15 493.15 368.15 -125 -1094.495 8.756
H2 Hot 498.15 328.15 493.15 323.15 -170 -402.863 2.370
C1 Cold 298.15 328.15 298.15 328.15 30 25.011 0.834
C2 Cold 328.15 393.15 328.15 393.15 65 357.124 5.494
Shifted temperature for the hot and cold stream in Pinch Technology

51. Temperature
(K)
Enthalpy, ∆H
(KW)
493.15
393.15 563.15
368.15 140.79
Hot Cold
328.15 Utility -158.33 Utility
323.15 7.68
298.15 -20.84
Supply = 179.17
Reject = 711.62
Difference = -532.45
Heat transfer to and from utilities for each temperature interval

55. Streams
Manual Calculation
(kg/hr)
Simulation
(kg/hr)
Error Percentage
(%)
1 21487.9794 21487.9790 0.00
2 21487.9794 21487.979 0.00
3 25862.1917 25918.1794 0.22
4 25862.1917 25918.1794 0.22
5 25862.1917 25918.1794 0.22
6 25862.1917 25918.1794 0.22
7 25862.1917 25918.1794 0.22
8 25862.1917 25918.1794 0.22
9 1583.3995 1657.9077 4.71
10 1583.3995 1657.9077 4.71
11 15.834 17.8594 12.79
12 1567.5655 1640.0483 4.62

56. Streams Manual Calculation
(kg/hr)
Simulation
(kg/hr)
Error Percentage
(%)
13 2806.6468 2790.4650 0.58
14 4374.2123 4430.5131 1.29
15 4374.2123 4430.5131 1.29
16 24278.7922 24260.2717 0.08
17 12882.6244 12938.7256 0.44
18 11396.1678 11321.5461 0.65
19 11396.1678 11321.5461 0.65
20 12882.6244 12938.7256 0.44
21 12882.6244 12938.7256 0.44
22 630.4375 630.035 0.06
23 886.8017 756.042 14.75
24 12626.2602 12812.7186 1.48

57. THANK YOU

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