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. A hydrocarbon fraction containing mainly n-heptane is dehydrogenated to produce toluene and hydrogen. The dehydrogenation process takes place at 427°C and 120 kPa. Assume 100 kmol h−1 of feed (poor n-heptane) entering the reactor at 220°C. The dehydrogenation process is strongly endothermic, and the reactor is fire heated to hold its temperature at 427°C. The conversion of n-heptane in the reaction: C7H16 → C7H8 + 4H2 is 50%. The reaction products are cooled to 25°C and led to a phase separator where hydrogen is separated. n-Heptane and toluene are separated by extractive distillation using n-methyl-pyrolydon (NMP) as the solvent. A flowsheet of straight simulation of this process is shown in Figure 11.1. Assume that methane is combusted to cover the heat requirement of the process; outlet temperature of flue gases is 550°C, and the total heat losses in the process are 1 MW. Calculate the amount of methane required without process heat integration; how much methane can be saved if the heat of reaction and heat of flue gases are recovered and used in the process? For heat recovery of flue assume that they are vented to the atmosphere at 150°C. Design a possible scheme for process heat recovery. (25 1.00 94 1.00 VENT 93) (94) (112) 0.00 NMP 0.00 0.00 182 TOLUENE C7 0.00 (25) 0.00 220 H2 1.00 25 (427 0.70 1.00 SEP N-C7 S1 (25 HE1 S3 S2 25 0.00 REACTOR HE2 0.00 93 S6 S4 S5 0.00 C1 Temperature (°C) PUMP1 HE3 Vapor Fraction Figure 11.1 A simple straight simulation of n-heptane dehydrogenation (203) R-NMPH 0.00

. A hydrocarbon fraction containing mainly n-heptane is dehydrogenated to produce toluene and hydrogen. The dehydrogenation process takes place at 427°C and 120 kPa. Assume 100 kmol h−1 of feed (poor n-heptane) entering the reactor at 220°C. The dehydrogenation process is strongly endothermic, and the reactor is fire heated to hold its temperature at 427°C. The conversion of n-heptane in the reaction: C7H16 → C7H8 + 4H2 is 50%. The reaction products are cooled to 25°C and led to a phase separator where hydrogen is separated. n-Heptane and toluene are separated by extractive distillation using n-methyl-pyrolydon (NMP) as the solvent. A flowsheet of straight simulation of this process is shown in Figure 11.1. Assume that methane is combusted to cover the heat requirement of the process; outlet temperature of flue gases is 550°C, and the total heat losses in the process are 1 MW. Calculate the amount of methane required without process heat integration; how much methane can be saved if the heat of reaction and heat of flue gases are recovered and used in the process? For heat recovery of flue assume that they are vented to the atmosphere at 150°C. Design a possible scheme for process heat recovery. (25 1.00 94 1.00 VENT 93) (94) (112) 0.00 NMP 0.00 0.00 182 TOLUENE C7 0.00 (25) 0.00 220 H2 1.00 25 (427 0.70 1.00 SEP N-C7 S1 (25 HE1 S3 S2 25 0.00 REACTOR HE2 0.00 93 S6 S4 S5 0.00 C1 Temperature (°C) PUMP1 HE3 Vapor Fraction Figure 11.1 A simple straight simulation of n-heptane dehydrogenation (203) R-NMPH 0.00

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
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. A hydrocarbon fraction containing mainly n-heptane is dehydrogenated to produce toluene and hydrogen. The dehydrogenation process takes place at 427°C and 120 kPa. Assume 100 kmol h−1 of feed (poor n-heptane) entering the reactor at 220°C. The dehydrogenation process is strongly endothermic, and the reactor is fire heated to hold its temperature at 427°C. The conversion of n-heptane in the reaction: C7H16 → C7H8 + 4H2 is 50%. The reaction products are cooled to 25°C and led to a phase separator where hydrogen is separated. n-Heptane and toluene are separated by extractive distillation using n-methyl-pyrolydon (NMP) as the solvent. A flowsheet of straight simulation of this process is shown in Figure 11.1. Assume that methane is combusted to cover the heat requirement of the process; outlet temperature of flue gases is 550°C, and the total heat losses in the process are 1 MW. Calculate the amount of methane required without process heat integration; how much methane can be saved if the heat of reaction and heat of flue gases are recovered and used in the process? For heat recovery of flue assume that they are vented to the atmosphere at 150°C. Design a possible scheme for process heat recovery. (25 1.00 94 1.00 VENT 93) (94) (112) 0.00 NMP 0.00 0.00 182 TOLUENE C7 0.00 (25) 0.00 220 H2 1.00 25 (427 0.70 1.00 SEP N-C7 S1 (25 HE1 S3 S2 25 0.00 REACTOR HE2 0.00 93 S6 S4 S5 0.00 C1 Temperature (°C) PUMP1 HE3 Vapor Fraction Figure 11.1 A simple straight simulation of n-heptane dehydrogenation (203) R-NMPH 0.00
Transcribed Image Text:. A hydrocarbon fraction containing mainly n-heptane is dehydrogenated to produce toluene and hydrogen. The dehydrogenation process takes place at 427°C and 120 kPa. Assume 100 kmol h−1 of feed (poor n-heptane) entering the reactor at 220°C. The dehydrogenation process is strongly endothermic, and the reactor is fire heated to hold its temperature at 427°C. The conversion of n-heptane in the reaction: C7H16 → C7H8 + 4H2 is 50%. The reaction products are cooled to 25°C and led to a phase separator where hydrogen is separated. n-Heptane and toluene are separated by extractive distillation using n-methyl-pyrolydon (NMP) as the solvent. A flowsheet of straight simulation of this process is shown in Figure 11.1. Assume that methane is combusted to cover the heat requirement of the process; outlet temperature of flue gases is 550°C, and the total heat losses in the process are 1 MW. Calculate the amount of methane required without process heat integration; how much methane can be saved if the heat of reaction and heat of flue gases are recovered and used in the process? For heat recovery of flue assume that they are vented to the atmosphere at 150°C. Design a possible scheme for process heat recovery. (25 1.00 94 1.00 VENT 93) (94) (112) 0.00 NMP 0.00 0.00 182 TOLUENE C7 0.00 (25) 0.00 220 H2 1.00 25 (427 0.70 1.00 SEP N-C7 S1 (25 HE1 S3 S2 25 0.00 REACTOR HE2 0.00 93 S6 S4 S5 0.00 C1 Temperature (°C) PUMP1 HE3 Vapor Fraction Figure 11.1 A simple straight simulation of n-heptane dehydrogenation (203) R-NMPH 0.00
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