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.
Software and Systems Engineering Standards: Verification and Validation of Sy...
Β
Production of 100 mt distilled monoglyceride (dmg)
1. SAJJAD KHUDHUR ABBAS
Ceo , Founder & Head of SHacademy
Chemical Engineering , Al-Muthanna University, Iraq
Oil & Gas Safety and Health Professional β OSHACADEMY
Trainer of Trainers (TOT) - Canadian Center of Human
Development
Episode 75 :PRODUCTION OF
100MT DISTILLED MONOGLYCERIDE
(DMG)
2.
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
4.
5.
6.
7. β’ Glycerolysis procedure is more economical -
fats are cheaper and less glycerol is required.
β’ Fats and fatty acids are insoluble in glycerol -
high temperatures are required to force the
reaction to proceed.
β’ On production scale, direct esterification and
interesterification can be done continuously
or batchwise.
8.
9.
10. COMPONENTS Appearance Formula
MW
(g/mol)
Tb
(K)
Tf
(K)
ΞfHo
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
11.
12. Proposed Process Batch Continuous
β’ Operating 24 hr/day
β’ Production is
continuous
β’ Total batch time 3-5 hours
β’ 7 batches/day production
β’ Operating 24 hr/day
β’ Production is
continuous
β’ 99% purity β’ 40 - 60% purity β’ 98% purity
β’ Annual cost is higher β’ Annual cost is lower β’ Annual cost is higher
β’ Lower maintenance
cost
β’ Higher specific
manufacturing and
operating cost
β’ Higher maintenance
cost
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.
39. β’ Determination of Minimum Number of Stages
β’ Minimum and Actual Reflux Ratio
π πππ =
πππ
π πΏπΎ
π π»πΎ
π π»πΎ
π πΏπΎ
ππππΌ π
π πππ =
πππ
π₯ πΏπ»π
π ππ»πΎπ
β πΌ πΏπΎ,π»πΎ
π π»πΎπ
π πΏπΎ
πΌ πΏπΎ,π»πΎ
β1
40. β’ Theoretical and Actual Number of Stages
β The theoretical number of stages, N is calculated by using Gilliland
correlation:
β’ Calculated column diameter D = 4.9388 m
β’ Column Height = 17.0688 m
π΅ β π΅ π΄π°π΅
π΅ + π
= π β πππ
π + ππ. ππ
π + πππ. ππ
π β π
π
44. β’ Where;
A = capacity or size parameter of the equipment
K1, K2, K3 = values used in the correlation
πππ10 πΆ π
π = πΎ1 + πΎ2 πππ10 π΄ + πΎ3[πππ10 π΄ ]2
48. Stream Type Tsupply (K)
Ttarget
(K)
Total Heat
Capacity
Flowrate, FCp
(KW/K)
Enthalpy
Change,
βH (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 βT βH 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
50.
51. Temperature
(K)
Enthalpy, βH
(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