Assuming that the feed mixture is liquid at its boiling O Calculate the flowrates (mol/hr) of the distillate and bottoms. D Determine the theoretical number of trays and the feed tray number for the specified operation. O Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux. Assuming that the feed mixture is saturated vapor determine ... ) Determine the theoretical number of trays and the feed tray number for the specified operation. =) Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux. Methyl Acetate-Ethyl Benzene System. A feed of 1000 mol/hr containing 40 mole % methyl acetate and 60 mole % ethyl benzene is to be froctionated at 101.325kPa (abs) in order to form a distillate containing 90 mole % methyl acetate and a thul acetate. The reflux ratio used is 5.0:1. Equilibrium for the system
Assuming that the feed mixture is liquid at its boiling O Calculate the flowrates (mol/hr) of the distillate and bottoms. D Determine the theoretical number of trays and the feed tray number for the specified operation. O Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux. Assuming that the feed mixture is saturated vapor determine ... ) Determine the theoretical number of trays and the feed tray number for the specified operation. =) Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux. Methyl Acetate-Ethyl Benzene System. A feed of 1000 mol/hr containing 40 mole % methyl acetate and 60 mole % ethyl benzene is to be froctionated at 101.325kPa (abs) in order to form a distillate containing 90 mole % methyl acetate and a thul acetate. The reflux ratio used is 5.0:1. Equilibrium for the system
Introduction to Chemical Engineering Thermodynamics
8th Edition
ISBN:9781259696527
Author:J.M. Smith Termodinamica en ingenieria quimica, Hendrick C Van Ness, Michael Abbott, Mark Swihart
Publisher:J.M. Smith Termodinamica en ingenieria quimica, Hendrick C Van Ness, Michael Abbott, Mark Swihart
Chapter1: Introduction
Section: Chapter Questions
Problem 1.1P
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Transcribed Image Text:Assuming that the feed mixture is liquid at its boiling point (e.g. a saturated llyu
) Calculate the flowrates (mol/hr) of the distillate and bottoms.
) Determine the theoretical number of trays and the feed tray number for the specified operation.
:) Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux.
Assuming that the feed mixture is saturated vapor determine ...
d) Determine the theoretical number of trays and the feed tray number for the specified operation.
e) Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux.
Methyl Acetate-Ethyl Benzene System.
A feed of 1000 mol/hr containing 40 mole % methyl acetate and 60 mole % ethyl benzene is to be
fractionated at 101.325kPa (abs) in order to form a distillate containing 90 mole % methyl acetate and a
bottoms containing 10.0 mole % methyl acetate. The reflux ratio used is 5.0:1. Equilibrium for the system
at 101.325kPa are available.
Assuming that the feed mixture is liquid at its boiling point (e.g. a saturated liquid) determine ...o
a) Calculate the flowrates (mol/hr) of the distillate and bottoms.
b) Determine the theoretical number of trays and the feed tray number for the specified operation.
c) Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux.
ul Assuming that the feed mixture is saturated vapor
determine .
...
d) Determine the theoretical number of trays and the feed tray number for the specified operation.
e) Determine the minimum reflux ratio, RMIN and the minimum number of theoretical trays at total reflux.
unOouraged as a tool useful to solve the problems.
Transcribed Image Text:Methyl Acetate Ethyl Benzene
at 1atm (101.325kPa)
Temperature
Methyl Acetate
T (K)
136.2
409.3
00 0 0
00 0 0
124.0
397.2
0.050
0.323
114.4
387.5
0.100
0.518
106.6
379.8
0.150
0.643
100.2
373.3
0.200
0.728
94.7
367.8
0.250
0.788
363.1
0.300
0.833
85.9
359.0
0.350
9986
82.3
355.4
0.400
0.892
352.2
0.450
0.912
76.1
349.3
0.500
0.929
73.5
346.6
0.550
0.942
71.0
344.2
0.953
68.8
342.0
0.650
0.963
66.8
339.9
0.700
0.971
64.9
338.0
0.750
0.977
63.1
336.2
0.800
0.983
61.4
334.6
0.850
0.988
59.9
333.0
0.993
58.4
331.5
0.950
0.997
57.0
330.1
to w0 0
to w0 0
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