Decanter 10X
Production of Glycerol Monostearate (KK1)Level 1-4
Presentation
Output ComponentsBoiling Point (C)Light key/Heavy
keyDestination
PFD 1Purification ofGlycerolPure Glycerol422.63Heavy keyMain
productMethanol64.7Heavy keyPurge and By productAsh, NaCI1465Heavy
keyPurge and by productFat (Stearic acid)376Heavy
keypurgeNaOCH3300Heavy keypurgeHCI108Heavy
keypurgeSteam/water100Heavy keyBiomassPFD 2Productionof
glycerolmonostearateGlycerol Monostearate422.63Heavy keyMain
ProductDistearate490.12Heavy keyRecycleTristearin813Heavy
keyRecycleGlycerol290Heavy keyRecycleHexane68Heavy
keyPurgeSteam/water100Heavy keyBiomassGlycerol + Tristearin
Glycerol Monostearate + DistearateGlycerol + Distearate 2 Glycerol
Monostearate Reaction EquationSodium Methoxide + HCl NaCl +
MethanolIn Neutralization ReactorIn Interesterification
ReactorEsterificationvsInteresterificationPotential for water
formation (soaping)1 mol of glycerol 1 mole of GMS- High reaction
speedNo water formation0.67 mol of glycerol 1 mol of GMSSpray
Dryer
PFD 1 Purification of Crude GlycerolReactor 1CentrifugeDecanter
1Phase separator 2Phase separator 1T = 200oCP = 6.8 barExothermic
reactionGlycerol = 60%Methanol = 32.6%NaOCH3 = 2.6%Fat = 2%Ash =
2.8%Purity = 98%
PFD 2 Production of Glycerol MonostearateDecanter 1Decanter
2Spray DryerReactor 1T = 200oCP = 2.5 barCatalyst = NaOH
PelletsExothermic reaction
WaterDesign Level 3* two reactors for two reactions take place*
both is CSTRHEAT EFFECT ON REACTOR
REACTOR 1 REACTOR 2VOLUME DESIGNREACTOR 2
Cost of reactor neutralization1. CSTR for Purification
Reactions-volume 30 m3, D=2.7m L=5.4m, the cost : RM1.09 million
using stainless steel
2. CSTR for Production of GMS- volume 12 m3, D=2m L=4m, the cost
: RM 461 thousand using carbon steel
Highest conversion for adiabatic equilibrium temperature, Xe =
0.27- thus, isothermal reaction is most preferred to increase yield
of conversion.Process purification (PFD1)Process Production
glycerol monostearate (PFD2)
fEP3=RM 177 million/year` Purification of glycerolTwo Phase
Separator 1CentrifugeDecanterTwo Phase Separator 2Production of
GMSDecanter 2Decanter 3Spray Dryer
SeparatorsIMSK is Marshall and Swift Cost index for 2012,
IMSK=1576.1
Decanter 1
Two Phase Separator
2CentrifugeGlycerolMethanolNaOCH3FatsAshWaterMethanolGlycerolNaOCH3FatsAshWater
Two Phase Separator 1WaterGlycerolWaterGlycerol
GlycerolMethanolWaterFatsAshHClNaOCH3NaClGlycerolWaterFatsMethanolHClNaOCH3AshNaClGlycerolWaterMethanolFatsHClNaOCH3GlycerolMethanolFatsWaterHClNaOCH3Diameter
of vessel,D = 0.92mLength of vessel,L = 2.76mVolumetric
Flowrate,Ql= 0.81m3/hrEconomic cost = RM 238 thousandDiameter of
vessel,D = 0.92 mLength of vessel,L = 2.76 mVolumetric Flowrate =
0.0028 m3/hrEconomic cost = RM 169 thousandEconomic cost = RM 28
thousandDiameter of vessel,D = 1.52 mLength of vessel,L = 3.04
mVolumetric Flowrate,Ql = 39.75m3/hrArea of vessel,A =
22.0m2Economic cost = RM 11 thousandDecanter 103HexaneGMS
HexaneGMS
Decanter 102Spray Dryer
HexaneGMSDisterateTristearinGlycerol
HexaneGMS
DisterateTristearinGlycerol
GMSWaterAirExhaust airGMSDiameter of vessel, D = 1.41 mLength of
vessel, L = 2.82 mDiameter of vessel, D = 1.66 mLength of vessel, L
= 3.32 m
Feed rate = 4382.2 kg/hInlet air temperature = 140C Outlet air
temperature = 90CInlet temperature of feed = 40CDischarge
temperature = 50C
Economic cost = RM 32 thousand Economic cost = RM 19 thousand
Economic cost = RM 337 thousand Diameter of vessel, D = 4.85
mHeight of cylindrical vessel, hcyl = 2.91 mHeight of cone, hcone=
3.47 m
Economic Potential for Level 4fEP 4 = RM 116 million/year
