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A saturated liquid feed of 500 mol/h at the boiling point contains 30 mol% ethanol and 70% water is to be fractionated at 101.32 kPa abs to give a distillate containing 90% ethanol and bottoms containing 3% ethanol. The reflux ratio used is 2.5:1. a. Calculate the amounts and compositions of distillate and bottom products, theoretical number of trays and the feed tray number. b. Determine the actual tray number of trays needed If the Murphree tray efficiency is 0.6 and also calculate the overall tray efficiency. (Use eq. data from App. A.3-23 Equilibrium data for ethanol-water system at 101.32 kPa (1 Atm).)

A saturated liquid feed of 500 mol/h at the boiling point contains 30 mol% ethanol and 70% water is to be fractionated at 101.32 kPa abs to give a distillate containing 90% ethanol and bottoms containing 3% ethanol. The reflux ratio used is 2.5:1. a. Calculate the amounts and compositions of distillate and bottom products, theoretical number of trays and the feed tray number. b. Determine the actual tray number of trays needed If the Murphree tray efficiency is 0.6 and also calculate the overall tray efficiency. (Use eq. data from App. A.3-23 Equilibrium data for ethanol-water system at 101.32 kPa (1 Atm).)

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
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A saturated liquid feed of 500 mol/h at the boiling point contains 30 mol% ethanol and 70% water is to be fractionated at 101.32 kPa abs to give a distillate containing 90% ethanol and bottoms containing 3% ethanol. The reflux ratio used is 2.5:1. a. Calculate the amounts and compositions of distillate and bottom products, theoretical number of trays and the feed tray number. b. Determine the actual tray number of trays needed If the Murphree tray efficiency is 0.6 and also calculate the overall tray efficiency. (Use eq. data from App. A.3-23 Equilibrium data for ethanol-water system at 101.32 kPa (1 Atm).)
Transcribed Image Text:A saturated liquid feed of 500 mol/h at the boiling point contains 30 mol% ethanol and 70% water is to be fractionated at 101.32 kPa abs to give a distillate containing 90% ethanol and bottoms containing 3% ethanol. The reflux ratio used is 2.5:1. a. Calculate the amounts and compositions of distillate and bottom products, theoretical number of trays and the feed tray number. b. Determine the actual tray number of trays needed If the Murphree tray efficiency is 0.6 and also calculate the overall tray efficiency. (Use eq. data from App. A.3-23 Equilibrium data for ethanol-water system at 101.32 kPa (1 Atm).)
A.3-23 Equilibrium Data for Ethanol-Water System at 101.325 kPa (1 Atm)* Vapor-Liquid Equilibria, Mass Fraction Ethanol Vapor-Liquid Equilibria, Mass Fraction Ethanol Enthalpy (btu/lb_ of mixture) Enthaipy (kJ/kg of mixture) Temperature Temperature Тетрerature Mass °C "F °C °F °C °F Fraction Liquid V apor Liquid Vapor 418.9 371.7 314.0 285.9 258.4 100.0 91.8 100.0 212 81.0 177.8 0.600 0.794 212 180.1 1150 2675 197.2 2517 0.192 0.377 0.527 0.656 0.713 0.822 0.858 80.1 176.2 0.1 159.8 1082 0.700 0.800 0.900 0.020 98.1 208.5 95.2 203.4 91.8 197.2 87.3 189.2 135.0 943 2193 0.050 0.100 0.200 79.1 174.3 84.7 184.5 0.3 1870 179.6 176.2 173.0 173.0 78.3 173.0 0.912 82.0 0.5 122.9 804 78.2 172.8 0.940 0.942 80.1 0.7 111.1 664 1544 224.7 1223 172.7 172.8 96.6 89.0 526 457.5 84.7 184.5 0.300 78.1 0.960 0.959 78.3 0.9 · 207.0. 0.978 1.00 78.3 1.0 1064 83.2 181.7 82.0 179.6 0.400 0.500 0.746 78.2 0.980 0.771 78.3 173.0 1.00 • Reference state for enthalpy is pure liquid at 273 K or 0"C. Source: Data from L. W. Cornell and R. E. Montonna, Ind. Eng. Chem., 25, 1331 (1933); and W. A. Noyes and R. R. Warfel, J. Am. Chem. Soc., 23, 463 (1901), as given by G. G. Brown, Unit Operations. New York: John Wiley & Sons, Inc., 1950. With permission.
Transcribed Image Text:A.3-23 Equilibrium Data for Ethanol-Water System at 101.325 kPa (1 Atm)* Vapor-Liquid Equilibria, Mass Fraction Ethanol Vapor-Liquid Equilibria, Mass Fraction Ethanol Enthalpy (btu/lb_ of mixture) Enthaipy (kJ/kg of mixture) Temperature Temperature Тетрerature Mass °C "F °C °F °C °F Fraction Liquid V apor Liquid Vapor 418.9 371.7 314.0 285.9 258.4 100.0 91.8 100.0 212 81.0 177.8 0.600 0.794 212 180.1 1150 2675 197.2 2517 0.192 0.377 0.527 0.656 0.713 0.822 0.858 80.1 176.2 0.1 159.8 1082 0.700 0.800 0.900 0.020 98.1 208.5 95.2 203.4 91.8 197.2 87.3 189.2 135.0 943 2193 0.050 0.100 0.200 79.1 174.3 84.7 184.5 0.3 1870 179.6 176.2 173.0 173.0 78.3 173.0 0.912 82.0 0.5 122.9 804 78.2 172.8 0.940 0.942 80.1 0.7 111.1 664 1544 224.7 1223 172.7 172.8 96.6 89.0 526 457.5 84.7 184.5 0.300 78.1 0.960 0.959 78.3 0.9 · 207.0. 0.978 1.00 78.3 1.0 1064 83.2 181.7 82.0 179.6 0.400 0.500 0.746 78.2 0.980 0.771 78.3 173.0 1.00 • Reference state for enthalpy is pure liquid at 273 K or 0"C. Source: Data from L. W. Cornell and R. E. Montonna, Ind. Eng. Chem., 25, 1331 (1933); and W. A. Noyes and R. R. Warfel, J. Am. Chem. Soc., 23, 463 (1901), as given by G. G. Brown, Unit Operations. New York: John Wiley & Sons, Inc., 1950. With permission.
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