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Problem 3 Consider a 700 mol/h feed entering a flash distillation unit or still under isothermal conditions containing 55 mole% of toluene and the rest is benzene. Operation of the still is at 760 torr. Additional data: Equilibrium data for the benzene-toluene system can be approximated with a constant relative volatility of 2.5, where benzene is the more volatile component. .) Plot the y - x diagram for benzene-toluene. (a) (b) ( ) If 60% of the feed is evaporated, find the liquid and vapor compositions (c) ( ..) If we desire a V/F of 0.60, what is the corresponding liquid composition and what are the liquid and vapor flow rates? 1 A. (d) (e- Find the compositions and flow rates of all unknown streams for a two stage flash cascade where 40% of the feed is flashed in the first stage and the liquid product is sent to a second flash chamber where 30% is flashed.

Problem 3 Consider a 700 mol/h feed entering a flash distillation unit or still under isothermal conditions containing 55 mole% of toluene and the rest is benzene. Operation of the still is at 760 torr. Additional data: Equilibrium data for the benzene-toluene system can be approximated with a constant relative volatility of 2.5, where benzene is the more volatile component. .) Plot the y - x diagram for benzene-toluene. (a) (b) ( ) If 60% of the feed is evaporated, find the liquid and vapor compositions (c) ( ..) If we desire a V/F of 0.60, what is the corresponding liquid composition and what are the liquid and vapor flow rates? 1 A. (d) (e- Find the compositions and flow rates of all unknown streams for a two stage flash cascade where 40% of the feed is flashed in the first stage and the liquid product is sent to a second flash chamber where 30% is flashed.

Introduction to Chemical Engineering Thermodynamics
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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Problem 3 Consider a 700 mol/h feed entering a flash distillation unit or still under isothermal conditions containing 55 mole% of toluene and the rest is benzene. Operation of the still is at 760 torr. Additional data: Equilibrium data for the benzene-toluene system can be approximated with a constant relative volatility of 2.5, where benzene is the more volatile component. .) Plot the y - x diagram for benzene-toluene. (a) (b) ( ) If 60% of the feed is evaporated, find the liquid and vapor compositions (c) ( .) If we desire a V/F of 0.60, what is the corresponding liquid composition and what are the liquid and vapor flow rates? COL (d) (---. Find the compositions and flow rates of all unknown streams for a two stage flash cascade where 40% of the feed is flashed in the first stage and the liquid product is sent to a second flash chamber where 30% is flashed.
Transcribed Image Text:Problem 3 Consider a 700 mol/h feed entering a flash distillation unit or still under isothermal conditions containing 55 mole% of toluene and the rest is benzene. Operation of the still is at 760 torr. Additional data: Equilibrium data for the benzene-toluene system can be approximated with a constant relative volatility of 2.5, where benzene is the more volatile component. .) Plot the y - x diagram for benzene-toluene. (a) (b) ( ) If 60% of the feed is evaporated, find the liquid and vapor compositions (c) ( .) If we desire a V/F of 0.60, what is the corresponding liquid composition and what are the liquid and vapor flow rates? COL (d) (---. Find the compositions and flow rates of all unknown streams for a two stage flash cascade where 40% of the feed is flashed in the first stage and the liquid product is sent to a second flash chamber where 30% is flashed.
Ness, H.C., and Abbott, M.M.] [from "Introduction to Chemical Engineering Thermodynamics (7th ed) by Smith, J.M., Van K (or DePriester) Chart (low T range) in American Engineering Units --100 -90 Methane 1 ********** isobutane 80 Ethylene Ethane سٹ Propylene Propane m n-Butane . in 300 7 015 -50 Isopentane ܤ ܗ ܘ 004- 200 n-Pentane -02 .005- .006- 00 .007 150 سلسل stynnying tour 5 E-03 008- -600 1 Pressure (psia) 04 015- سل......سلا Temperature (°F) i n-Hexane .02- F015 n-Heptane 2 20 6000 fringing .03- 001 5 02 do to Ivelantander las bandantiandunud 8 سلسل tantuntutuntudnutent 6 6 0068 8 016 8 سلسليسلسل tundmalin 02 n-Octane n-Nonane 0006 S 20- S SO 5 987 سلسلسلسا 4 15 14.7 6 6 5 8 تبيليسسلسلسيليسيليسيليسيليسيلسلسلسلسسلسلسبلسلسسلسسلسل Methane Ethylene Ethane Propylene Propane Isobutane n-Butane Isopentane n-Pentane N gragaumgang 3 n-Hexane n-Heptane n-Octane n-Nonane
Transcribed Image Text:Ness, H.C., and Abbott, M.M.] [from "Introduction to Chemical Engineering Thermodynamics (7th ed) by Smith, J.M., Van K (or DePriester) Chart (low T range) in American Engineering Units --100 -90 Methane 1 ********** isobutane 80 Ethylene Ethane سٹ Propylene Propane m n-Butane . in 300 7 015 -50 Isopentane ܤ ܗ ܘ 004- 200 n-Pentane -02 .005- .006- 00 .007 150 سلسل stynnying tour 5 E-03 008- -600 1 Pressure (psia) 04 015- سل......سلا Temperature (°F) i n-Hexane .02- F015 n-Heptane 2 20 6000 fringing .03- 001 5 02 do to Ivelantander las bandantiandunud 8 سلسل tantuntutuntudnutent 6 6 0068 8 016 8 سلسليسلسل tundmalin 02 n-Octane n-Nonane 0006 S 20- S SO 5 987 سلسلسلسا 4 15 14.7 6 6 5 8 تبيليسسلسلسيليسيليسيليسيليسيلسلسلسلسسلسلسبلسلسسلسسلسل Methane Ethylene Ethane Propylene Propane Isobutane n-Butane Isopentane n-Pentane N gragaumgang 3 n-Hexane n-Heptane n-Octane n-Nonane
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