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shift reactor unit (Unit 1300) is designed to convert CO to CO2 for future operation. A process flow diagram for a water-gas shift (WGS) reaction system is shown in Figure B.12.1. The stream table and equipment summary are in Table B.12.1 and Table B.12.3, respectively. The objective of the process is to achieve an overall 90% conversion of CO in the process. Based on the PFD, estimate the total module cost and the grassroots cost in year 2016 for the plant. Due to increasing of production, an additional of the similar Unit 1300 has been considered in year 2020. To observe the cost changes until 2020, show a trend plot of grassroots cost between year 2017 and 2020, and calculate the percentage difference in cost for an additional of the Unit 1300 made in 2020 compared to 2016? Remark: Use suitable references for Chemical Engineering Plant Cost Index (CEPCI) in order to estimate the cost.

shift reactor unit (Unit 1300) is designed to convert CO to CO2 for future operation. A process flow diagram for a water-gas shift (WGS) reaction system is shown in Figure B.12.1. The stream table and equipment summary are in Table B.12.1 and Table B.12.3, respectively. The objective of the process is to achieve an overall 90% conversion of CO in the process. Based on the PFD, estimate the total module cost and the grassroots cost in year 2016 for the plant. Due to increasing of production, an additional of the similar Unit 1300 has been considered in year 2020. To observe the cost changes until 2020, show a trend plot of grassroots cost between year 2017 and 2020, and calculate the percentage difference in cost for an additional of the Unit 1300 made in 2020 compared to 2016? Remark: Use suitable references for Chemical Engineering Plant Cost Index (CEPCI) in order to estimate the cost.

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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A shift reactor unit (Unit 1300) is designed to convert CO to CO2 for future operation. A process flow diagram for a water-gas shift (WGS) reaction system is shown in Figure B.12.1. The stream table and equipment summary are in Table B.12.1 and Table B.12.3, respectively. The objective of the process is to achieve an overall 90% conversion of CO in the process. Based on the PFD, estimate the total module cost and the grassroots cost in year 2016 for the plant. Due to increasing of production, an additional of the similar Unit 1300 has been considered in year 2020. To observe the cost changes until 2020, show a trend plot of grassroots cost between year 2017 and 2020, and calculate the percentage difference in cost for an additional of the Unit 1300 made in 2020 compared to 2016?


Remark: Use suitable references for Chemical Engineering Plant Cost Index (CEPCI) in order to estimate the cost.

 

Table B.12.1 Stream Table for Unit 1300 Stream Number Temperature (°C) Pressure (bar) Vapor fraction Mass flow (kg/h) Mole flow (kmol/h) Component flowrates (kmol/h) CO CO₂ H₂ H₂O Heat Exchangers E-1301 A = 67.2 m² 1 E-1302 2 A = 31.7 m 115 16.7 1.0 2191.2 100.0 31.3 27.7 40.2 0.8 Floating head, carbon steel, shell- and-tube design Process stream in tubes. Q = 1580 MJ/h Maximum pressure rating of 19 bar Floating head, carbon steel, shell- and-tube design Process stream in tubes Q = 455 MJ/h Maximum pressure rating of 19 bar 3 320 15.2 1.0 2191.2 100.0 31.3 27.7 40.2 0.8 E-1303 A = 62.2 m² 4 325 16.2 1.0 1678.3 93.2 0.0 0.0 0.0 93.2 6 319.7 15.2 1.0 3869.5 193.2 31.3 27.7 40.2 94.0 Floating head, carbon steel, shell- and-tube design Process stream in shell Q = 3764 MJ/h Maximum pressure rating of 19 bar Stream Number Temperature (°C) Pressure (bar) Vapor fraction Mass flow (kg/h) Mole flow (kmol/h) Table B.12.3 Major Equipment Summary for Unit 1300 Component flowrates (kmol/h) CO 00₂ H₂ H₂O Reactors R-1301 Carbon steel, chromia-promoted iron oxide catalyst Catalyst bed height = 2.8 m Diameter = 0.75 m Maximum pressure rating of 19 bar Maximum allowable catalyst temperature = 477°C Vessel V-1301 Vertical Carbon steel Length = 1.83 m Diameter = 0.61 m Maximum pressure rating of 19 bar Fired Heater H-1301 Vertical Required heat load = 696 MJ/h Design (maximum) heat load = 800 MJ/h 75% thermal efficiency Maximum pressure rating of 19 bar 7 425.1 14.7 1.0 11.6 47-4 8 59.9 74-3 250.1 3869.5 193.2 193.2 13.8 1.0 3869.5 3.1 55-9 9 50 12.7 1.0 2705.0 128.6 3.1 55-9 68.4 68.4 65.8 1.2 R-1302 Carbon steel, copper-zinc oxide catalyst Catalyst bed height = 1.9 m Diameter 0.75 m Maximum pressure rating of 19 bar Maximum allowable catalyst temperature = 288°C 10 50 11.7 0.0 1164.5 64.6 0.0 0.0 0.0 64.6
Transcribed Image Text:Table B.12.1 Stream Table for Unit 1300 Stream Number Temperature (°C) Pressure (bar) Vapor fraction Mass flow (kg/h) Mole flow (kmol/h) Component flowrates (kmol/h) CO CO₂ H₂ H₂O Heat Exchangers E-1301 A = 67.2 m² 1 E-1302 2 A = 31.7 m 115 16.7 1.0 2191.2 100.0 31.3 27.7 40.2 0.8 Floating head, carbon steel, shell- and-tube design Process stream in tubes. Q = 1580 MJ/h Maximum pressure rating of 19 bar Floating head, carbon steel, shell- and-tube design Process stream in tubes Q = 455 MJ/h Maximum pressure rating of 19 bar 3 320 15.2 1.0 2191.2 100.0 31.3 27.7 40.2 0.8 E-1303 A = 62.2 m² 4 325 16.2 1.0 1678.3 93.2 0.0 0.0 0.0 93.2 6 319.7 15.2 1.0 3869.5 193.2 31.3 27.7 40.2 94.0 Floating head, carbon steel, shell- and-tube design Process stream in shell Q = 3764 MJ/h Maximum pressure rating of 19 bar Stream Number Temperature (°C) Pressure (bar) Vapor fraction Mass flow (kg/h) Mole flow (kmol/h) Table B.12.3 Major Equipment Summary for Unit 1300 Component flowrates (kmol/h) CO 00₂ H₂ H₂O Reactors R-1301 Carbon steel, chromia-promoted iron oxide catalyst Catalyst bed height = 2.8 m Diameter = 0.75 m Maximum pressure rating of 19 bar Maximum allowable catalyst temperature = 477°C Vessel V-1301 Vertical Carbon steel Length = 1.83 m Diameter = 0.61 m Maximum pressure rating of 19 bar Fired Heater H-1301 Vertical Required heat load = 696 MJ/h Design (maximum) heat load = 800 MJ/h 75% thermal efficiency Maximum pressure rating of 19 bar 7 425.1 14.7 1.0 11.6 47-4 8 59.9 74-3 250.1 3869.5 193.2 193.2 13.8 1.0 3869.5 3.1 55-9 9 50 12.7 1.0 2705.0 128.6 3.1 55-9 68.4 68.4 65.8 1.2 R-1302 Carbon steel, copper-zinc oxide catalyst Catalyst bed height = 1.9 m Diameter 0.75 m Maximum pressure rating of 19 bar Maximum allowable catalyst temperature = 288°C 10 50 11.7 0.0 1164.5 64.6 0.0 0.0 0.0 64.6
Steam Syngas H-1301 Syngas Heater T(°C) P (bar) R-1301 First-Stage WGS Reactor poc H-1301 air ng E-1301 Interstage Cooler 203 14.2 3 R-1301 R-1302 6 R-1302 Second-Stage WGS Reactor E-1301 E-1303 E-1302 8 E-1302 E-1303 Low-Pressure Reactor Effluent Cooler Steam Generator 50 12.8 185 13.2 V-1301 Shifted Syngas Separator 9 V-1301 Figure B.12.1 Unit 1300: Shift Reactor Process Flow Diagram Shifted Syngas Condensate to Wastewater Treatment Unit
Transcribed Image Text:Steam Syngas H-1301 Syngas Heater T(°C) P (bar) R-1301 First-Stage WGS Reactor poc H-1301 air ng E-1301 Interstage Cooler 203 14.2 3 R-1301 R-1302 6 R-1302 Second-Stage WGS Reactor E-1301 E-1303 E-1302 8 E-1302 E-1303 Low-Pressure Reactor Effluent Cooler Steam Generator 50 12.8 185 13.2 V-1301 Shifted Syngas Separator 9 V-1301 Figure B.12.1 Unit 1300: Shift Reactor Process Flow Diagram Shifted Syngas Condensate to Wastewater Treatment Unit
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