major products. At industrial scale, ethylbenzene is produced via various production routes. The most widely known route is the alkylation of ethylene (AEO). Since alkylation of ethylene is an established process, as a beginner in ethylbenzene production in Malaysia, ChemMaju Sdn. Bhd. is planning to produce ethylbenzene via this route. The production capacity is expected to be around 40, 000 MTPA of ethylbenzene. Although AEO is an established process, it has a drawback in which the production of ethylbenzene is accompanied by the production of styrene as an undesired product: CaH,CH, + 2 CHa → CH;C,Hs + C3He (Equation 1- Main reaction) CaHsCaHs CaHs + H2 (Equation 2 - Side reaction) As the lead process engineer in ChemMaju Sdn. Bhd., you are given the task to design of an ethylbenzene production plant. Your first step is to lead your team in designing the reactor for the alkylation of ethylene process. In order to save cost, you proposed to use a non-catalytic, adiabatic flow reactor. Since the reaction is non-catalytic, the process should be a thermal process to ensure its thermodynamic feasibility, with minimum required inlet reaction temperature of 227 °C. The homogeneous reaction is in gas phase, with constant total pressure of 7.5 atm. The reaction of the reactants is 1:2 (toluene: ethylene) based on stoichiometric ratio. However, the feed is 1:4 (toluene: ethylene), making it insufficient toluene to consume all the ethylene. Therefore, toluene is the limiting reactant for the basis of calculation. Task 1 By assuming that the side reaction is negligible at the reaction temperature, conduct a detailed design of a) an adiabatic CSTR and b) an adiabatic PFR for the non-catalytic, alkylation of ethylene process. The designed reactors must achieve 90% conversion. Then, with critical analysis and justification, choose the most appropriate reactor (between the designed CSTR and PFR) for the process. Given that, 50,132- ka,Cn, = 44.32 exp (- RT 42,741 keMiC,Muforward = 5.13 exp RT
major products. At industrial scale, ethylbenzene is produced via various production routes. The most widely known route is the alkylation of ethylene (AEO). Since alkylation of ethylene is an established process, as a beginner in ethylbenzene production in Malaysia, ChemMaju Sdn. Bhd. is planning to produce ethylbenzene via this route. The production capacity is expected to be around 40, 000 MTPA of ethylbenzene. Although AEO is an established process, it has a drawback in which the production of ethylbenzene is accompanied by the production of styrene as an undesired product: CaH,CH, + 2 CHa → CH;C,Hs + C3He (Equation 1- Main reaction) CaHsCaHs CaHs + H2 (Equation 2 - Side reaction) As the lead process engineer in ChemMaju Sdn. Bhd., you are given the task to design of an ethylbenzene production plant. Your first step is to lead your team in designing the reactor for the alkylation of ethylene process. In order to save cost, you proposed to use a non-catalytic, adiabatic flow reactor. Since the reaction is non-catalytic, the process should be a thermal process to ensure its thermodynamic feasibility, with minimum required inlet reaction temperature of 227 °C. The homogeneous reaction is in gas phase, with constant total pressure of 7.5 atm. The reaction of the reactants is 1:2 (toluene: ethylene) based on stoichiometric ratio. However, the feed is 1:4 (toluene: ethylene), making it insufficient toluene to consume all the ethylene. Therefore, toluene is the limiting reactant for the basis of calculation. Task 1 By assuming that the side reaction is negligible at the reaction temperature, conduct a detailed design of a) an adiabatic CSTR and b) an adiabatic PFR for the non-catalytic, alkylation of ethylene process. The designed reactors must achieve 90% conversion. Then, with critical analysis and justification, choose the most appropriate reactor (between the designed CSTR and PFR) for the process. Given that, 50,132- ka,Cn, = 44.32 exp (- RT 42,741 keMiC,Muforward = 5.13 exp RT
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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Transcribed Image Text:major products.
At industrial scale, ethylbenzene is produced via various production routes. The
most widely known route is the alkylation of ethylene (AEO). Since alkylation of
ethylene is an established process, as a beginner in ethylbenzene production in
Malaysia, ChemMaju Sdn. Bhd. is planning to produce ethylbenzene via this route. The
production capacity is expected to be around 40, 000 MTPA of ethylbenzene. Although
AEO is an established process, it has a drawback in which the production of
ethylbenzene is accompanied by the production of styrene as an undesired product:
CoHsCH3 + 2 C2H4 → CeHsC2Hs + C3H6
(Equation 1 - Main reaction)
CeHsC2Hs ++ CaHs + H2
(Equation 2 - Side reaction)
As the lead process engineer in ChemMaju Sdn. Bhd., you are given the task to design
of an ethylbenzene production plant. Your first step is to lead your team in designing
the reactor for the alkylation of ethylene process. In order to save cost, you proposed
to use a non-catalytic, adiabatic flow reactor. Since the reaction is non-catalytic, the
process should be a thermal process to ensure its thermodynamic feasibility, with
minimum required inlet reaction temperature of 227 °C. The homogeneous reaction is
in gas phase, with constant total pressure of 7.5 atm. The reaction of the reactants is
1:2 (toluene: ethylene) based on stoichiometric ratio. However, the feed is 1:4 (toluene:
ethylene), making it insufficient toluene to consume all the ethylene. Therefore, toluene
is the limiting reactant for the basis of calculation.
Task 1
By assuming that the side reaction is negligible at the reaction temperature, conduct a
detailed design of a) an adiabatic CSTR and b) an adiabatic PFR for the non-catalytic,
alkylation of ethylene process. The designed reactors must achieve 90% conversion.
Then, with critical analysis and justification, choose the most appropriate reactor
(between the designed CSTR and PFR) for the process. Given that,
50,132:
mo
kcall,CH; = 44.32 exp (-
RT
42,741 mol
kcsCHaforward = 5.13 exp
RT
68,496
kclt,C,Hareverse = 255.3 exp
mol
RT
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