Vapor Liquid Downflow area, A4 (from tray above) Downflow area, A (to tray below) Active area, A. Total area, A= A, + 244 Ул K, 2.759 1.225 Component 0.2971 0.4631 0.3521 0.1700 0.1459 0.4677 0.1802 1.0000 0.4290 0.3865 0.2398 1.0000 0.4010 1.0000 0.3673 04676 1.0000

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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The following results were obtained for Tray n from a rate-basedcalculation of a ternary distillation at 14.7 psia, involving acetone (1), methanol (2), and water (3) in a 5.5-ft-diameter column using sieve trays with a 2-inch-high weir. Vapor and liquid phases are assumed to be completely mixed.The computed products of the gas-phase, binary mass-transfer coefficients
and interfacial area, using the Chan–Fair correlation of §6.6,are as follows in lbmol/:
k12 =k21=1, 955; k13 =k31 =2,407; k23=k32 = 2,797
(a) Compute the molar diffusion rates. (b) Compute the masstransfer
rates. (c) Calculate the Murphree vapor-tray efficiencies.

Vapor
Liquid
Downflow
area, A4
(from tray
above)
Downflow
area, A
(to tray
below)
Active
area, A.
Total area, A= A, + 244
Transcribed Image Text:Vapor Liquid Downflow area, A4 (from tray above) Downflow area, A (to tray below) Active area, A. Total area, A= A, + 244
Ул
K,
2.759
1.225
Component
0.2971
0.4631
0.3521
0.1700
0.1459
0.4677
0.1802
1.0000
0.4290
0.3865
0.2398
1.0000
0.4010
1.0000
0.3673
04676
1.0000
Transcribed Image Text:Ул K, 2.759 1.225 Component 0.2971 0.4631 0.3521 0.1700 0.1459 0.4677 0.1802 1.0000 0.4290 0.3865 0.2398 1.0000 0.4010 1.0000 0.3673 04676 1.0000
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