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Key Points Non-Isothermal Reactor Design Effect of AT on KA, -rA, XA, # or W отр MB > RL » Stoich > DP-> DT Energy Balance: Q-Ws-Fro Edilpi (T-To) - FAOXA [Dax + DCCT-TR)] = (==) SYS Q: I've when added Ws: tve when leaving change in temp DHRx Eviti Species change in chemical Adiabatic operation বद ་ DG Evile Q=0 7 Consider the reversible, exothermic, gas phase reaction 2A → B + C in a flow reactor. Pure A enters at 300 K, and the maximum operating temperature is 600 K. FA0 = 8 mol/min, Kc = 50 at 320 K, KA = 0.2 L/mol min at 400 K, EA = 12,000 cal/mol, vo = 2 L/min. Pressure drop is negligible. Species A H (273 K) -18 kcal/mol Ср 40 cal/mol.K B -36 kcal/mol 40 cal/mol K C -32 kcal/mol 40 cal/mol.K 1. Calculate the conversion and temperature in a 60 L adiabatic CSTR. Hint: If you are having problems getting Polymath to converge on a solution, use initial guesses for X and T that both fall on the same Energy Balance line.

Key Points Non-Isothermal Reactor Design Effect of AT on KA, -rA, XA, # or W отр MB > RL » Stoich > DP-> DT Energy Balance: Q-Ws-Fro Edilpi (T-To) - FAOXA [Dax + DCCT-TR)] = (==) SYS Q: I've when added Ws: tve when leaving change in temp DHRx Eviti Species change in chemical Adiabatic operation বद ་ DG Evile Q=0 7 Consider the reversible, exothermic, gas phase reaction 2A → B + C in a flow reactor. Pure A enters at 300 K, and the maximum operating temperature is 600 K. FA0 = 8 mol/min, Kc = 50 at 320 K, KA = 0.2 L/mol min at 400 K, EA = 12,000 cal/mol, vo = 2 L/min. Pressure drop is negligible. Species A H (273 K) -18 kcal/mol Ср 40 cal/mol.K B -36 kcal/mol 40 cal/mol K C -32 kcal/mol 40 cal/mol.K 1. Calculate the conversion and temperature in a 60 L adiabatic CSTR. Hint: If you are having problems getting Polymath to converge on a solution, use initial guesses for X and T that both fall on the same Energy Balance line.

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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Please help me! Especially with the polymath
Key Points Non-Isothermal Reactor Design Effect of AT on KA, -rA, XA, # or W отр MB > RL » Stoich > DP-> DT Energy Balance: Q-Ws-Fro Edilpi (T-To) - FAOXA [Dax + DCCT-TR)] = (==) SYS Q: I've when added Ws: tve when leaving change in temp DHRx Eviti Species change in chemical Adiabatic operation বद ་ DG Evile Q=0 7
Transcribed Image Text:Key Points Non-Isothermal Reactor Design Effect of AT on KA, -rA, XA, # or W отр MB > RL » Stoich > DP-> DT Energy Balance: Q-Ws-Fro Edilpi (T-To) - FAOXA [Dax + DCCT-TR)] = (==) SYS Q: I've when added Ws: tve when leaving change in temp DHRx Eviti Species change in chemical Adiabatic operation বद ་ DG Evile Q=0 7
Consider the reversible, exothermic, gas phase reaction 2A → B + C in a flow reactor. Pure A enters at 300 K, and the maximum operating temperature is 600 K. FA0 = 8 mol/min, Kc = 50 at 320 K, KA = 0.2 L/mol min at 400 K, EA = 12,000 cal/mol, vo = 2 L/min. Pressure drop is negligible. Species A H (273 K) -18 kcal/mol Ср 40 cal/mol.K B -36 kcal/mol 40 cal/mol K C -32 kcal/mol 40 cal/mol.K 1. Calculate the conversion and temperature in a 60 L adiabatic CSTR. Hint: If you are having problems getting Polymath to converge on a solution, use initial guesses for X and T that both fall on the same Energy Balance line.
Transcribed Image Text:Consider the reversible, exothermic, gas phase reaction 2A → B + C in a flow reactor. Pure A enters at 300 K, and the maximum operating temperature is 600 K. FA0 = 8 mol/min, Kc = 50 at 320 K, KA = 0.2 L/mol min at 400 K, EA = 12,000 cal/mol, vo = 2 L/min. Pressure drop is negligible. Species A H (273 K) -18 kcal/mol Ср 40 cal/mol.K B -36 kcal/mol 40 cal/mol K C -32 kcal/mol 40 cal/mol.K 1. Calculate the conversion and temperature in a 60 L adiabatic CSTR. Hint: If you are having problems getting Polymath to converge on a solution, use initial guesses for X and T that both fall on the same Energy Balance line.
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