A gas phase catalytic reaction is performed in a fluidized bed operating at a superficial gas velocity of 0.3 m/s. For this reaction under these conditions it is known that the reaction is first order in reactant A. The following information is given: W bed height at incipient fluidization = 1.5 m; • operating mean bed height = 1.65m; voidage at incipient fluidization = 0.47; • reaction rate constant = 75.47 (per unit volume of solids); Umf = 0.033 m/s; • mean bubble rise velocity = 0.111 m/s; mass transfer coefficient between bubbles and emulsion 0.1009 (based on unit bubble volume) minimum fluidization velocity = 0.033 m/s. Use the reactor model of Orcutt et al. to determine: (a) the conversion of reactant A; (b) the effect on the conversion found in (a) of reducing the inventory of catalyst by one half; (c) the effect on the conversion found in (a) of halving the bubble size (assuming the interphase mass transfer coefficient is inversely proportional to the square root of the bubble diameter).
A gas phase catalytic reaction is performed in a fluidized bed operating at a superficial gas velocity of 0.3 m/s. For this reaction under these conditions it is known that the reaction is first order in reactant A. The following information is given: W bed height at incipient fluidization = 1.5 m; • operating mean bed height = 1.65m; voidage at incipient fluidization = 0.47; • reaction rate constant = 75.47 (per unit volume of solids); Umf = 0.033 m/s; • mean bubble rise velocity = 0.111 m/s; mass transfer coefficient between bubbles and emulsion 0.1009 (based on unit bubble volume) minimum fluidization velocity = 0.033 m/s. Use the reactor model of Orcutt et al. to determine: (a) the conversion of reactant A; (b) the effect on the conversion found in (a) of reducing the inventory of catalyst by one half; (c) the effect on the conversion found in (a) of halving the bubble size (assuming the interphase mass transfer coefficient is inversely proportional to the square root of the bubble diameter).
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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A gas phase catalytic reaction is performed in a fluidized bed operating at a superficial gas velocity of 0.3 m/s. For this reaction under these conditions it is known that the reaction is first order in reactant A. The following information is given: W bed height at incipient fluidization = 1.5 m; • operating mean bed height = 1.65m; voidage at incipient fluidization = 0.47; • reaction rate constant = 75.47 (per unit volume of solids); Umf = 0.033 m/s; • mean bubble rise velocity = 0.111 m/s; mass transfer coefficient between bubbles and emulsion 0.1009 (based on unit bubble volume) minimum fluidization velocity = 0.033 m/s. Use the reactor model of Orcutt et al. to determine: (a) the conversion of reactant A; (b) the effect on the conversion found in (a) of reducing the inventory of catalyst by one half; (c) the effect on the conversion found in (a) of halving the bubble size (assuming the interphase mass transfer coefficient is inversely proportional to the square root of the bubble diameter).
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