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Q2. An aqueous glucose stream is to be catalytically hydrogenated to produce sorbitol in a CSTR. Feed to the reactor consists of an aqueous glucose stream (2.6 kg mol/m³) and a 120% of stoichiometric hydrogen gas stream. The reactor is operated isothermally at 423 K and at a pressure of 10,000 kPa, leading to solubility of hydrogen to be 5 kg mol/m³. The rate of reaction was found to be 8.59 x 10 kg mol/m³/s under such conditions. If the conversion achieved in this CSTR is 66%, estimate the flow rate of glucose stream for a 3 m³ volume of CSTR. Neglect the mass transfer effects.

Q2. An aqueous glucose stream is to be catalytically hydrogenated to produce sorbitol in a CSTR. Feed to the reactor consists of an aqueous glucose stream (2.6 kg mol/m³) and a 120% of stoichiometric hydrogen gas stream. The reactor is operated isothermally at 423 K and at a pressure of 10,000 kPa, leading to solubility of hydrogen to be 5 kg mol/m³. The rate of reaction was found to be 8.59 x 10 kg mol/m³/s under such conditions. If the conversion achieved in this CSTR is 66%, estimate the flow rate of glucose stream for a 3 m³ volume of CSTR. Neglect the mass transfer effects.

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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Q2. An aqueous glucose stream is to be catalytically hydrogenated to produce sorbitol in a CSTR. Feed to the reactor consists of an aqueous glucose stream (2.6 kg mol/m³) and a 120% of stoichiometric hydrogen gas stream. The reactor is operated isothermally at 423 K and at a pressure of 10,000 kPa, leading to solubility of hydrogen to be 5 kg mol/m³. The rate of reaction was found to be 8.59 x 104 kg mol/m³/s under such conditions. If the conversion achieved in this CSTR is 66%, estimate the flow rate of glucose stream for a 3 m³ volume of CSTR. Neglect the mass transfer effects. Q3. It is desired to produce ethylene by thermal cracking of ethane at a rate of 875 mol/h. The reaction takes place at 1500 °F and 50 psia. C2H6 > C2H4 + H2 C2H6 > 0.5 C2H4 +CH4 moles of ethylene formed 1- 0.038 The selectivity is given as S = moles of ethane converted (1–x)0.24 The cost of ethylene is $6.15/mol and that of ethane is $1.65/mol. Fuel cost is $4/MMBtu. Fuel values of hydrogen and methane are 1.23 and 0.383 MMBtu/mol, respectively. Draw the input-output structure of the flowsheet and find the economic potential when the per pass conversion is 0.2.
Transcribed Image Text:Q2. An aqueous glucose stream is to be catalytically hydrogenated to produce sorbitol in a CSTR. Feed to the reactor consists of an aqueous glucose stream (2.6 kg mol/m³) and a 120% of stoichiometric hydrogen gas stream. The reactor is operated isothermally at 423 K and at a pressure of 10,000 kPa, leading to solubility of hydrogen to be 5 kg mol/m³. The rate of reaction was found to be 8.59 x 104 kg mol/m³/s under such conditions. If the conversion achieved in this CSTR is 66%, estimate the flow rate of glucose stream for a 3 m³ volume of CSTR. Neglect the mass transfer effects. Q3. It is desired to produce ethylene by thermal cracking of ethane at a rate of 875 mol/h. The reaction takes place at 1500 °F and 50 psia. C2H6 > C2H4 + H2 C2H6 > 0.5 C2H4 +CH4 moles of ethylene formed 1- 0.038 The selectivity is given as S = moles of ethane converted (1–x)0.24 The cost of ethylene is $6.15/mol and that of ethane is $1.65/mol. Fuel cost is $4/MMBtu. Fuel values of hydrogen and methane are 1.23 and 0.383 MMBtu/mol, respectively. Draw the input-output structure of the flowsheet and find the economic potential when the per pass conversion is 0.2.
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