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a. Determine the distillate and bottoms flow rates (in moles). b. Determine the number of equilibrium stages required when a reflux ratio of 1.5 is used. Determine the slope and intercept for the top operating line. c. Determine the minimum number of stages required for the desired separation. d. Determine the minimum reflux.

a. Determine the distillate and bottoms flow rates (in moles). b. Determine the number of equilibrium stages required when a reflux ratio of 1.5 is used. Determine the slope and intercept for the top operating line. c. Determine the minimum number of stages required for the desired separation. d. Determine the minimum reflux.

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 2. A fractionation column operating at 1 bar is to separate 10,000 kg/hr of a mixture of benzene and ethylbenzene containing 71.62 mass percent ethylbenzene into an overhead product containing 94.63 mass percent benzene and a bottoms product containing 95.50 mass percent ethylbenzene. The feed is liquid at its boiling point, feed is on the optimum tray, and the reflux is at saturation temperature. The column has a total condenser and a partial reboiler. a. Determine the distillate and bottoms flow rates (in moles). b. Determine the number of equilibrium stages required when a reflux ratio of 1.5 is used. Determine the slope and intercept for the top operating line. c. Determine the minimum number of stages required for the desired separation. d. Determine the minimum reflux. It is not necessary to determine the number of fractional stages in parts b and c. Must plot the equilibrium curve using a spreadsheet for parts b and c, but can step off the stages by hand on the printed graph. Table 1. Vapor-liquid equilibrium data for the benzene (1)/ethylbenzene (2) system at 1 bar. T, °C X₁ 135.679 130.13 125.126 120.594 116.472 112.707 109.254 106.075 103.138 100.415 97.883 95.521 93.313 91.242 89.297 87.466 85.739 84.106 82.561 81.095 79.703 У1 0 0 0.05 0.18382 0.1 0.32872 0.15 0.2 0.25 0.3 0.35 0.4 0.45 0.5 0.9 0.95 1 0.44436 0.53774 0.61395 0.67679 0.72908 0.77296 0.81008 0.84171 0.55 0.86882 0.6 0.89221 0.65 0.9125 0.7 0.93018 0.75 0.94567 0.8 0.9593 0.85 0.97133 0.982 0.99151
Transcribed Image Text:Problem 2. A fractionation column operating at 1 bar is to separate 10,000 kg/hr of a mixture of benzene and ethylbenzene containing 71.62 mass percent ethylbenzene into an overhead product containing 94.63 mass percent benzene and a bottoms product containing 95.50 mass percent ethylbenzene. The feed is liquid at its boiling point, feed is on the optimum tray, and the reflux is at saturation temperature. The column has a total condenser and a partial reboiler. a. Determine the distillate and bottoms flow rates (in moles). b. Determine the number of equilibrium stages required when a reflux ratio of 1.5 is used. Determine the slope and intercept for the top operating line. c. Determine the minimum number of stages required for the desired separation. d. Determine the minimum reflux. It is not necessary to determine the number of fractional stages in parts b and c. Must plot the equilibrium curve using a spreadsheet for parts b and c, but can step off the stages by hand on the printed graph. Table 1. Vapor-liquid equilibrium data for the benzene (1)/ethylbenzene (2) system at 1 bar. T, °C X₁ 135.679 130.13 125.126 120.594 116.472 112.707 109.254 106.075 103.138 100.415 97.883 95.521 93.313 91.242 89.297 87.466 85.739 84.106 82.561 81.095 79.703 У1 0 0 0.05 0.18382 0.1 0.32872 0.15 0.2 0.25 0.3 0.35 0.4 0.45 0.5 0.9 0.95 1 0.44436 0.53774 0.61395 0.67679 0.72908 0.77296 0.81008 0.84171 0.55 0.86882 0.6 0.89221 0.65 0.9125 0.7 0.93018 0.75 0.94567 0.8 0.9593 0.85 0.97133 0.982 0.99151
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