Ex. 9.3. In the design of a process, separate liquid streams of pure species A and B will enter a CSTR, where they will be consumed by the irreversible reaction: 2A+B → C where ra =k,c,cB k, = 24.7 ft / lbmol hr, c,Cz in lbmol / ft speciesA:nA =110lbmol / hr (MW = 59lb,, / lbmol) speciesB:nB = 68lbmol / hr (MW =133lb,, / lbmol) In the reactor, 90% of species A is to be reacted, and the output stream will have a density of 50.5lb, / ft . What volume must the reactor have? A: 110 lbmol/hr, 59 lb, Ilbmol B: 68 lbmol/hr, 133 lb,/lbmol 2A+B→C fut rate = (24.7 ft°/lbmol•hr) c4 CB 90% conversion of A 50.5 lb„ft, V. out Reactor Volume = V
Ex. 9.3. In the design of a process, separate liquid streams of pure species A and B will enter a CSTR, where they will be consumed by the irreversible reaction: 2A+B → C where ra =k,c,cB k, = 24.7 ft / lbmol hr, c,Cz in lbmol / ft speciesA:nA =110lbmol / hr (MW = 59lb,, / lbmol) speciesB:nB = 68lbmol / hr (MW =133lb,, / lbmol) In the reactor, 90% of species A is to be reacted, and the output stream will have a density of 50.5lb, / ft . What volume must the reactor have? A: 110 lbmol/hr, 59 lb, Ilbmol B: 68 lbmol/hr, 133 lb,/lbmol 2A+B→C fut rate = (24.7 ft°/lbmol•hr) c4 CB 90% conversion of A 50.5 lb„ft, V. out Reactor Volume = V
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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![**Example 9.3**
In the design of a process, separate liquid streams of pure species A and B will enter a Continuous Stirred-Tank Reactor (CSTR), where they will be consumed by the irreversible reaction:
\[ 2A + B \rightarrow C \]
where
\[ r_A = k_r c_A c_B \]
- \( k_r = 24.7 \text{ ft}^3/\text{lbmol hr} \),
- \( c_A, c_B \) in lbmol/ft\(^3\).
\[
\text{species A: } n_A = 110 \text{ lbmol/hr } \quad (MW = 59 \text{ lb}_m/\text{lbmol})
\]
\[
\text{species B: } n_B = 68 \text{ lbmol/hr } \quad (MW = 133 \text{ lb}_m/\text{lbmol})
\]
In the reactor, 90% of species A is to be reacted, and the output stream will have a density of \( 50.5 \text{ lb}_m/\text{ft}^3 \). What volume must the reactor have?
**Diagram Explanation:**
In the diagram, there is a depiction of a reactor with inputs and an output stream. The inputs include:
- Species A: 110 lbmol/hr with a molar weight of 59 lb\(_m\)/lbmol.
- Species B: 68 lbmol/hr with a molar weight of 133 lb\(_m\)/lbmol.
The reaction taking place is \( 2A + B \rightarrow C \) with a rate of \( 24.7 \text{ ft}^3/\text{lbmol hr} \). The setup ensures a 90% conversion of A. The output stream from the reactor has a density of \( 50.5 \text{ lb}_m/\text{ft}^3 \), and the system's objective is to determine the necessary volume \( V \) of the reactor.](/v2/_next/image?url=https%3A%2F%2Fcontent.bartleby.com%2Fqna-images%2Fquestion%2F8c0357bc-c66f-4e55-895d-285c7a4f1ce5%2Fe9c23da3-4091-4031-89e4-4ebdf7d67a12%2F2ojd3ad_processed.png&w=3840&q=75)
Transcribed Image Text:**Example 9.3**
In the design of a process, separate liquid streams of pure species A and B will enter a Continuous Stirred-Tank Reactor (CSTR), where they will be consumed by the irreversible reaction:
\[ 2A + B \rightarrow C \]
where
\[ r_A = k_r c_A c_B \]
- \( k_r = 24.7 \text{ ft}^3/\text{lbmol hr} \),
- \( c_A, c_B \) in lbmol/ft\(^3\).
\[
\text{species A: } n_A = 110 \text{ lbmol/hr } \quad (MW = 59 \text{ lb}_m/\text{lbmol})
\]
\[
\text{species B: } n_B = 68 \text{ lbmol/hr } \quad (MW = 133 \text{ lb}_m/\text{lbmol})
\]
In the reactor, 90% of species A is to be reacted, and the output stream will have a density of \( 50.5 \text{ lb}_m/\text{ft}^3 \). What volume must the reactor have?
**Diagram Explanation:**
In the diagram, there is a depiction of a reactor with inputs and an output stream. The inputs include:
- Species A: 110 lbmol/hr with a molar weight of 59 lb\(_m\)/lbmol.
- Species B: 68 lbmol/hr with a molar weight of 133 lb\(_m\)/lbmol.
The reaction taking place is \( 2A + B \rightarrow C \) with a rate of \( 24.7 \text{ ft}^3/\text{lbmol hr} \). The setup ensures a 90% conversion of A. The output stream from the reactor has a density of \( 50.5 \text{ lb}_m/\text{ft}^3 \), and the system's objective is to determine the necessary volume \( V \) of the reactor.
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