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P8-4A Consider the following system of gas-phase reactions: -1 •min Tx = k,C k = 0.004(mol/dm³)" -r A → X A → B r = k,C, k, = 0.3 min¬1 A » Y ry = k,C k, = 0.25 dm³/mol · min B is the desired product, and X and Y are foul pollutants that are expensive to get rid of. The specific reaction rates are at 27°C. The reaction system is to be operated at 27°C and 4 atm. Pure A enters the system at a volumetric flow rate of 10 dm³/min. (a) Sketch the instantaneous selectivities (SB/x, SB/Y, and Sp/xY = rg/(rx+ry)) as a function of the con- centration of Ca- (b) Consider a series of reactors. What should be the volume of the first reactor? (c) What are the effluent concentrations of A, B, X, and Y from the first reactor? (d) What is the conversion of A in the first reactor? (e) If 99% conversion of A is desired, what reaction scheme and reactor sizes should you use to max- imize SB/XY? (f) Suppose that E, = 20,000 cal/mol, E, = 10,000 cal/mol, and Ez = 30,000 cal/mol. What temperature would of A of 0.1 mol/dm? (g) If you could vary the pressure between 1 and 100 atm, what pressure would you choose? l you recommend for a single CSTR with a space time of 10 min and an entering concentration

P8-4A Consider the following system of gas-phase reactions: -1 •min Tx = k,C k = 0.004(mol/dm³)" -r A → X A → B r = k,C, k, = 0.3 min¬1 A » Y ry = k,C k, = 0.25 dm³/mol · min B is the desired product, and X and Y are foul pollutants that are expensive to get rid of. The specific reaction rates are at 27°C. The reaction system is to be operated at 27°C and 4 atm. Pure A enters the system at a volumetric flow rate of 10 dm³/min. (a) Sketch the instantaneous selectivities (SB/x, SB/Y, and Sp/xY = rg/(rx+ry)) as a function of the con- centration of Ca- (b) Consider a series of reactors. What should be the volume of the first reactor? (c) What are the effluent concentrations of A, B, X, and Y from the first reactor? (d) What is the conversion of A in the first reactor? (e) If 99% conversion of A is desired, what reaction scheme and reactor sizes should you use to max- imize SB/XY? (f) Suppose that E, = 20,000 cal/mol, E, = 10,000 cal/mol, and Ez = 30,000 cal/mol. What temperature would of A of 0.1 mol/dm? (g) If you could vary the pressure between 1 and 100 atm, what pressure would you choose? l you recommend for a single CSTR with a space time of 10 min and an entering concentration

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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P8-4A Consider the following system of gas-phase reactions: -1 •min Tx = k,C k = 0.004(mol/dm³)" -r A → X A → B r = k,C, k, = 0.3 min¬1 A » Y ry = k,C k, = 0.25 dm³/mol · min B is the desired product, and X and Y are foul pollutants that are expensive to get rid of. The specific reaction rates are at 27°C. The reaction system is to be operated at 27°C and 4 atm. Pure A enters the system at a volumetric flow rate of 10 dm³/min. (a) Sketch the instantaneous selectivities (SB/x, SB/Y, and Sp/xY = rg/(rx+ry)) as a function of the con- centration of Ca- (b) Consider a series of reactors. What should be the volume of the first reactor? (c) What are the effluent concentrations of A, B, X, and Y from the first reactor? (d) What is the conversion of A in the first reactor? (e) If 99% conversion of A is desired, what reaction scheme and reactor sizes should you use to max- imize SB/XY? (f) Suppose that E, = 20,000 cal/mol, E, = 10,000 cal/mol, and Ez = 30,000 cal/mol. What temperature would of A of 0.1 mol/dm³? (g) If you could vary the pressure between 1 and 100 atm, what I you recommend for a single CSTR with a space time of 10 min and an entering concentration pressure would you choose?
Transcribed Image Text:P8-4A Consider the following system of gas-phase reactions: -1 •min Tx = k,C k = 0.004(mol/dm³)" -r A → X A → B r = k,C, k, = 0.3 min¬1 A » Y ry = k,C k, = 0.25 dm³/mol · min B is the desired product, and X and Y are foul pollutants that are expensive to get rid of. The specific reaction rates are at 27°C. The reaction system is to be operated at 27°C and 4 atm. Pure A enters the system at a volumetric flow rate of 10 dm³/min. (a) Sketch the instantaneous selectivities (SB/x, SB/Y, and Sp/xY = rg/(rx+ry)) as a function of the con- centration of Ca- (b) Consider a series of reactors. What should be the volume of the first reactor? (c) What are the effluent concentrations of A, B, X, and Y from the first reactor? (d) What is the conversion of A in the first reactor? (e) If 99% conversion of A is desired, what reaction scheme and reactor sizes should you use to max- imize SB/XY? (f) Suppose that E, = 20,000 cal/mol, E, = 10,000 cal/mol, and Ez = 30,000 cal/mol. What temperature would of A of 0.1 mol/dm³? (g) If you could vary the pressure between 1 and 100 atm, what I you recommend for a single CSTR with a space time of 10 min and an entering concentration pressure would you choose?
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