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CHE 397 Group Charlie Priya Chetty, Scott Morgan, Brian Mottel, Daniyal Qamar, Sukhjinder Singh

CHE 397 Group Charlie Priya Chetty, Scott Morgan, Brian Mottel, Daniyal Qamar, Sukhjinder Singh Mentor: Dennis O’ Brien Dr. Jeffery Perl. Agenda. Design Basis Chemistry PFD Flow Sheeting Energy Sinks/Loads Costing/Sizing. Design Basis.

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CHE 397 Group Charlie Priya Chetty, Scott Morgan, Brian Mottel, Daniyal Qamar, Sukhjinder Singh

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  1. CHE 397 Group Charlie Priya Chetty, Scott Morgan, Brian Mottel, Daniyal Qamar, Sukhjinder Singh Mentor: Dennis O’ Brien Dr. Jeffery Perl

  2. Agenda Design Basis Chemistry PFD Flow Sheeting Energy Sinks/Loads Costing/Sizing

  3. Design Basis Utilize the syngas provided by group Delta to synthesize Methanol Plant located in Chicago because of MSW 2300TPD syngas to produce 1600 TPD Methanol at a purity of 99.2 wt%

  4. Chemistry CO2 + H2 → CO + H2O ∆Hrxn = 17694 Btu/lbmol conversion: 0.1 of CO2 CO + 2H2 → CH3OH ∆Hrxn = 39037 Btu/lbmol Conversion: 0.4 of CO 2CO +4H2 → CH3CH2OH +H2O ∆Hrxn = 147033 Btu/lbmol Conversion: 0.01 of CO 4CO +8H2 → CH3CH2CH2CH2OH + 3H2O ∆Hrxn = 319862 Btu/lbmol conversion : 0.005

  5. Process Flow Diagram

  6. Methanol Production Heat exchanger: 45000 lb/hr inlet at 70F outlet 1090F Reactor: Pressure 1200 psi Temperature 518 F Turbo expander: Pressure drop of 452 psi

  7. Methanol purification Flash: 648psi, 118ºF, separates 97% of CO, 100% H2, 75% CO2 Valve: Reduces pressure from 648psi to 31psi Column 1: Separates ~100% CO, CO2 Column 2: Separates water, methanol, and higher alcohols to obtain 99.2% pure methanol Turbo Expander 2: Pressure drop of 16.3psi

  8. Flow Sheet

  9. Flow Sheet (cont.)

  10. Energy Sinks & Loads

  11. Equipment Sizing Reactor size: GHSV = volume feed/volume of reactor Volume of reactor with 3000 GHSV = 43 ft3 Mean Residence time = 1.19 s Flash Drum Size: Vmax = k[(ρl- ρv)/ ρl]^0.5 = 1.4 ft/s K for 600 psi = 0.3 Vol flow = 2.86 ft3/s Total Volume calculated = 3500 ft3 Heat Exchanger: A=Q/U∆Tlm With U value of 250 BTU/F Ft2 h, an average for evaporators and heaters A = 6681 ft2

  12. Continued

  13. Continued

  14. Property insurance is 0.5% of annual plant cost Property tax is 2% of annual plant cost

  15. RISK PROFILE FOR INVESTORS

  16. Solutions to questions from previous presentation 1.Cost of syngas 2.Assumptions -Mostly removed -Reactor has more reactions -Conversion/selectivity set for the reactions 3.Distillation pressure and drop -Pressure adjusted -Two columns -by products 4.Costs for equipment 5.Depriciation cost

  17. Improvements Add more reactors to simulate quenching Utilize membrane separators to purge off excess gasses Use water tubes to cool reactor Do sensitivity analysis to find out whether turbo expanders/heat exchangers are cost effective Increase Methanol purity

  18. Questions??

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