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5) Analysis of a binary, multi-stage distillation column results in the following equations for the operating lines: Rectification operating line: y₁ = 0.64x₁+1+0.29 Stripping operating line: Yi-1 = 1.9x; -0.015 The component molar flowrate of the more volatile component in the bottom product stream is 0.7 mol s1 and the feed molar flowrate is 60 mol s-1. Determine the following: = = iii) iv) v) The reflux ratio. The mole fraction of the more volatile component in the distillate. The molar flowrates of liquid and vapour in the stripping section of the column. The mole fraction of the more volatile component in the feed. The molar flowrates of liquid and vapour in the rectification section of the column. vi) The coordinates of the intersection of the operating lines. vii) The 'quality' of the feed.

5) Analysis of a binary, multi-stage distillation column results in the following equations for the operating lines: Rectification operating line: y₁ = 0.64x₁+1+0.29 Stripping operating line: Yi-1 = 1.9x; -0.015 The component molar flowrate of the more volatile component in the bottom product stream is 0.7 mol s1 and the feed molar flowrate is 60 mol s-1. Determine the following: = = iii) iv) v) The reflux ratio. The mole fraction of the more volatile component in the distillate. The molar flowrates of liquid and vapour in the stripping section of the column. The mole fraction of the more volatile component in the feed. The molar flowrates of liquid and vapour in the rectification section of the column. vi) The coordinates of the intersection of the operating lines. vii) The 'quality' of the feed.

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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Q5. i) R=1.78; ii)xd=0.81;; iii)Vs=46.7 mol/s; Ls=88.7 mol/s; iv) xf=0.25; vi)Vr=50 mol/s ,Lr=32 mol/s; v) x=0.242; y=0.445; vii)q=0.944

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5) Analysis of a binary, multi-stage distillation column results in the following equations for the operating lines: Rectification operating line: y₁ = 0.64x₁+1+0.29 Stripping operating line: Yi-1 =1.9x; -0.015 The component molar flowrate of the more volatile component in the bottom product stream is 0.7 mol s-1 and the feed molar flowrate is 60 mol s-¹. Determine the following: The reflux ratio. The mole fraction of the more volatile component in the distillate. The molar flowrates of liquid and vapour in the stripping section of the column. リ iv) v) vi) vii) The mole fraction of the more volatile component in the feed. The molar flowrates of liquid and vapour in the rectification section of the column. The coordinates of the intersection of the operating lines. The 'quality' of the feed.
Transcribed Image Text:5) Analysis of a binary, multi-stage distillation column results in the following equations for the operating lines: Rectification operating line: y₁ = 0.64x₁+1+0.29 Stripping operating line: Yi-1 =1.9x; -0.015 The component molar flowrate of the more volatile component in the bottom product stream is 0.7 mol s-1 and the feed molar flowrate is 60 mol s-¹. Determine the following: The reflux ratio. The mole fraction of the more volatile component in the distillate. The molar flowrates of liquid and vapour in the stripping section of the column. リ iv) v) vi) vii) The mole fraction of the more volatile component in the feed. The molar flowrates of liquid and vapour in the rectification section of the column. The coordinates of the intersection of the operating lines. The 'quality' of the feed.
My feeling is that this problem posed most difficulties. This was intended to be a challenging one. Much of this involved using the standard expressions for the Rectification Operating line (which we obtained from a component balance above the feed), L₁ -Xitl + V₁ V₂ and the Stripping Operating line (obtained from a component balance below the feed): Yi = Y₁ = Xitl V₂ D W V₂ xa, -Xw or yi R R+1 -Xitl + 1 R+1 -Xa We equated the gradient and intercept of the given operating lines to the relevant parts of these expressions, thus determining R and Xd. A key step was to interpret that the molar flowrate of the more volatile component in the bottom product stream was, 0.7 mol s¹¹, i.e. Wxw = 0.7 mol s¹. Thus, Vs could be found, leading to Ls. The bottom product flowrate could be found as the difference between Ls and Vs, allowing the distillate flowrate and feed composition to be found via total and component balances over the whole column. The intersection of the operating lines (or any two linear function) could be found by substituting one into the other. The feed quality, q, could be found by the relation between Lr and Ls, or by other equivalent approaches.
Transcribed Image Text:My feeling is that this problem posed most difficulties. This was intended to be a challenging one. Much of this involved using the standard expressions for the Rectification Operating line (which we obtained from a component balance above the feed), L₁ -Xitl + V₁ V₂ and the Stripping Operating line (obtained from a component balance below the feed): Yi = Y₁ = Xitl V₂ D W V₂ xa, -Xw or yi R R+1 -Xitl + 1 R+1 -Xa We equated the gradient and intercept of the given operating lines to the relevant parts of these expressions, thus determining R and Xd. A key step was to interpret that the molar flowrate of the more volatile component in the bottom product stream was, 0.7 mol s¹¹, i.e. Wxw = 0.7 mol s¹. Thus, Vs could be found, leading to Ls. The bottom product flowrate could be found as the difference between Ls and Vs, allowing the distillate flowrate and feed composition to be found via total and component balances over the whole column. The intersection of the operating lines (or any two linear function) could be found by substituting one into the other. The feed quality, q, could be found by the relation between Lr and Ls, or by other equivalent approaches.
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