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Use the pressure estimated in splitter operationto get estimates
on
1) Reflux Ratio, R
3) Number of theoretical stages, N4) Feed tray location
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The top product must be in vapor form to avoid
condensing ethane
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02210191305
5distillateinkeyHeavy
01160
503503659
9bottomsinkeyLight
.
.
Actual reflux ratio=1.75 Rm
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Number of trays = 16Feed entry tray: 8 or 9
Verify the distillate composition with the target
specification
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Select fullreflux
Number oftrays
Feed entry
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Assume negligible pressure drop in condenser
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Providing these values will speed up the calculations
Estimatesfrom short cutdistillation
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Providing these values will speed up the calculations
From shortcut distillation
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Move to Monitor page to solve the problem
Monitor
Specified
parameters
Helps to check
the progress
of simulation
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Need to re-adjust the pressure
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Make 8th tray as the feed entry tray
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Define two new component flows based on the
specifications of propane and butane in distillateand bottom
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Define propane from the distillate and butane from
bottom
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Define propane from the distillate and butane from
bottom
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Replace the default specifications of reflux ratio and
distillate flow rate with the new specifications andrun the
simulation
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Results are available on performance tab
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Results are available on performance tab
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Reaction parameters can be added to any
separation vessel including distillation column
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H83 PS1/H84 CFL
Separate Ethanol-Water azeotrope using ethyl
glycol with a column operating at atmosphericpressure with
negligible pressure drop
Feed of 100 kmol/hr is fed to the extractive columnat the
entrainer/feed ratio of 1
Entrainer is recovered in the entrainer recoverycolumn
The entrainer makeup flow M is small compared to
the total flow and must be balanced with theentrainer losses in
streams D1 and D2.
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Extractive column Entrainer recovery
column
Theoretical stages
CondenserUpper Feed
Lower Feed
Reboiler
19
12
20
1
3
5
Condenser Type total total
Reflux ratio 1.0 1.0
Distillate mole fractions
Ethanol
Water
Ethylene Glycol
0.9327
0.0673
0
0.3563
0.5439
0.0997Upper feed mole fractions
Ethanol
Water
Ethylene Glycol
0
0
1
Lower feed mole fractions
Ethanol
Water
Ethylene Glycol
0.8564
0.1436
0
Bottom mole fractions
Ethanol
Water
Ethylene Glycol
0.0492
0.0752
0.8756
0
0
1
Temperatures
Upper feed
Lower feed
78.29oC
78.12oC
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Here, the liquid phase is a non-ideal mixture. So,
activity models have to be selectedAssume ideal gas model for
vapor phase
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