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Overhead vapor, Ov Feed, F (Sat'd liquid) T-325 K P=2027 kPa Component kmol/h 163.3 108.9 272.2 Propylene Propane 90 150 Condenser, C Reflux drum 7-319.5 K Distillate, D (Sat'd liquid) P=1931 kPa Reflux, R 2293 kmol/h Column with contacting plates Boilup 2575 kmol/h Steam Condensate Reboller, R Component kmol/h Propylene 157.6 Propane 1.6 159.2 Bottoms, B (Sat'd liquid) T-330.9 K P-2069 kPa Component Propylene Propane kmol/h 5.7 107.3 113.0

Overhead vapor, Ov Feed, F (Sat'd liquid) T-325 K P=2027 kPa Component kmol/h 163.3 108.9 272.2 Propylene Propane 90 150 Condenser, C Reflux drum 7-319.5 K Distillate, D (Sat'd liquid) P=1931 kPa Reflux, R 2293 kmol/h Column with contacting plates Boilup 2575 kmol/h Steam Condensate Reboller, R Component kmol/h Propylene 157.6 Propane 1.6 159.2 Bottoms, B (Sat'd liquid) T-330.9 K P-2069 kPa Component Propylene Propane kmol/h 5.7 107.3 113.0

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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What is the volumetric flow rate in L/h of Feed in the attached picture? 

converting to the volume of the feed, show all steps, and be professional. 

The use All e. c. For a prox blems, tional sare 3 lists Those need r the aran- that im- -h as nvenient product degradation or undesirable agglomeration, a pilot- plant is necessary. Operations near the middle usually require laboratory data, while those near the bottom require pilot- plant tests. Feed, F (Sat'd liquid) T = 325 K P = 2027 kPa Sometimes Overhead vapor, OV Component kmol/h 163.3 108.9 272.2 Propylene Propane 1 90 150 Figure 1.16 Distillation of a propylene-propane mixture. points, they are traditionally separated by distillation. From Figure 1.16, it is seen that a large number of stages is needed and that the reflux and boilup flows are large. Accordingly, attention has been given to replacement of distillation with a more economical and less energy-intensive process. Based on the factors in Table 1.12, the characteristics in Table 1.13, and the list of species properties given at the end of $1.2, propose alternatives to Figure 1.16. Condenser, C CW Column with contacting plates Steam Reflux, R 2293 kmol/h Boilup 2575 kmol/h (Reflux drum Condensate Reboiler, R Distillate, D (Sat'd liquid) T-319.5 K P = 1931 kPa Component Propylene Propane Bottoms, B (Sat'd liquid) T-330.9 K P=2069 kPa Component Propylene Propane kmol/h 5.7 107.3 113.0 kmol/h 157.6 1.6 159.2
Transcribed Image Text:The use All e. c. For a prox blems, tional sare 3 lists Those need r the aran- that im- -h as nvenient product degradation or undesirable agglomeration, a pilot- plant is necessary. Operations near the middle usually require laboratory data, while those near the bottom require pilot- plant tests. Feed, F (Sat'd liquid) T = 325 K P = 2027 kPa Sometimes Overhead vapor, OV Component kmol/h 163.3 108.9 272.2 Propylene Propane 1 90 150 Figure 1.16 Distillation of a propylene-propane mixture. points, they are traditionally separated by distillation. From Figure 1.16, it is seen that a large number of stages is needed and that the reflux and boilup flows are large. Accordingly, attention has been given to replacement of distillation with a more economical and less energy-intensive process. Based on the factors in Table 1.12, the characteristics in Table 1.13, and the list of species properties given at the end of $1.2, propose alternatives to Figure 1.16. Condenser, C CW Column with contacting plates Steam Reflux, R 2293 kmol/h Boilup 2575 kmol/h (Reflux drum Condensate Reboiler, R Distillate, D (Sat'd liquid) T-319.5 K P = 1931 kPa Component Propylene Propane Bottoms, B (Sat'd liquid) T-330.9 K P=2069 kPa Component Propylene Propane kmol/h 5.7 107.3 113.0 kmol/h 157.6 1.6 159.2
Expert Solution
Step 1

Given:

The molar flow rate of the feed (propylene and propane) is given to us. We require the volume flow rate (in L/h) of the feed.

To calculate the volumetric flow rate, we need two quantities, the mass flow rate and the density of the substance, since the volume flow rate is given as follows:

Q = m.ρ

So, we need to calculate the density and the mass flow rate for both components first.

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