1 / 25

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. BLOCK FLOW DIAGRAM. Hot Feed. Recycle Stream. MS Compressor. HX. Splitter. Reactor. Condenser. Flash. Water. Cold Syngas. Crude Methanol.

keegan-rice
Download Presentation

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

An Image/Link below is provided (as is) to download presentation Download Policy: Content on the Website is provided to you AS IS for your information and personal use and may not be sold / licensed / shared on other websites without getting consent from its author. Content is provided to you AS IS for your information and personal use only. Download presentation by click this link. While downloading, if for some reason you are not able to download a presentation, the publisher may have deleted the file from their server. During download, if you can't get a presentation, the file might be deleted by the publisher.

E N D

Presentation Transcript

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

  2. BLOCK FLOW DIAGRAM Hot Feed Recycle Stream MS Compressor HX Splitter Reactor Condenser Flash Water Cold Syngas Crude Methanol Grade AA Methanol Low Key impurities Distillation I Distillation II Higher Alcohols

  3. Schematic Flow Diagram

  4. MATERIAL AND ENERGY BALANCESREACTOR

  5. Material and Energy Balance

  6. Material and Energy Balance

  7. HAND CALCULATIONS AND DATA REACTOR

  8. Reactor Material Balance Assumptions: 100% separation of all feed gases (CO, H2, CO2) and products (CH3OH, H2O) Purge Concentrations are controllable for now No Nitrogen or Water in feed syngas Other side reactions ignored Pressure effects on Cp

  9. Hand Calculations Reactor Reaction 1: CO +H2 ↔ CH3OH ΔHrxn = -38559 Btu/lbmol Reaction 2: CO2 +3H2 ↔ CH3OH + H20 ΔHrxn = -21324.1 Btu/lbmol Reaction 1 Conv = 0.5 Reaction 2 Conv = .04 Material Balance: COout = COfeed + COrec– .5(COfeed + COrec)– COpurge CO2out = (CO2 feed + CO2rec) – 0.04 (CO2 feed + CO2rec) – CO2 purge CH3OHout = .5(COout + COfeed) + .04(CO2out + CO2 feed) Energy Balance Enthalpy in (BTU) : H = Δ Href + ∫Cpdt for each component Where Cp was used for gases: Cp = A + BT + CT2 +DT3 Enthalpy of reaction = .5(ΔHrxn1)COin + .04(ΔHrxn2)CO2in

  10. Data Reactor

  11. MATERIAL AND ENERGY BALANCESDISTILLATION COLUMN

  12. Material Balance

  13. Energy Balance

  14. HAND CALCULATIONS AND DATA DISTILLATION COLUMN

  15. Distillation Column Material Balance Assumptions 7669.62 lb-Moles/Hr of Methanol/H20 in feed Feed composition 97.6% Methanol, 2.4% H20 Feed Pressure is 14.7psia 99.5% Methanol in Distillate

  16. Hand Calculations Distillation Column Material Balance F = B + D Fz = BxB + DxD Energy Balance Fhf + QC + QR = DhD +BhB Q = mCPΔT

  17. MATERIAL AND ENERGY BALANCEHEAT EXCHANGER

  18. MATERIAL BALANCE AND DATA for HEAT EXCHANGER

  19. Hand Calculations HX Q = Σ miCpiΔT T(Syngas in) = 482 ˚F T(Crude MeOH in) = 515 ˚F Crude MeOH in = 31.22 lbmol/hr Water in = .7554 lbmol/hr Syngas Compositions ( H2 = 6.6, CO = 3.2, CO2 = 2) Q = 31.22lbmol/hr(267)(482-515) +.7554lbmol/hr(271)(482-515) Q = -281834.9622 Btu/hr = 6.6(122)(T-482) + 3.2(126)(T-482) + 2(188)(T-482) = 8052T - 388106.4 + 403.2T – 194342.4 + 37.6T – 18123.2 281834.96 Btu/hr = 100 (125) (T-482) T(Syngas out) = 505 ˚F Cp Values (Btu/lbmol°F

  20. ECONOMIC ANALYSIS

  21. Fixed Capital CostTable 1.1: Estimate costs of specific units in the process flow diagram Amirkhas, Elton , and Raj Bedi. "METHANOL PRODUCTION IN TRINIDAD & TOBAGO." Phase II Design Report 07062006. n. pag. Web. 15 Feb 2011.

  22. Operating Cost Table 1.2: Estimate plant costs and operations Harkins, John. "WHAT IS UNDERGROUND COAL GASIFICATION (UCG)? ." Clean Global Energy (2010): n. pag. Web. 15 Feb 2011

  23. Capital InvestmentTable 1.3: Annual costs Bell, David, and Brian Towler. Coal Gasification and Its Applications. William Andrew, 2010. Print.

  24. Future Goals Include side reactions Account for by products Refine calculations using more accurate conditions Reaction kinetics Economics consistent with our project Distillation column specifics Sizing of equipment Heat exchangers and pumps Compressor

  25. QUESTIONS?

More Related