Download presentation
Presentation is loading. Please wait.
Published byCarmella Pitts Modified over 9 years ago
1
Production of Gasoline Components from Synthesis Gas ChE 397 Senior Design Group Alpha Ayesha Rizvi Bernard Hsu Jeff Tyska Mohammad Shehadeh Yacoub Awwad 2011.04.26
2
Overview Process Basics Block Flow Diagram Plant and Equipment Layout General Economics Conclusions and Further Improvements
3
Our Process H2H2
4
Process Equation 2H 2 + CO ZSM-5 C 5 + + H 2 O + LPG (C3/C4)
5
Why Gasoline and Mobil Process? Existing infrastructure Established and high demand product Great amount of C5+ gasoline in the final product Lower Gasoline Price Reduced Sox/GHG emissions Easy to scale Renewable feedstock Energy Independence SO 2
6
Competing Processes Fischer-Tropsch Oil Tar Sands (2n+1) H 2 + n CO → C n H(2n+2) + n H 2 O http://portland.indymedia.org/media/image s/2010/12/404850.jpg http://tonto.eia.doe.gov/country/index.cfm?view=production 43%
7
Process Summary Syngas Methanol Methanol Water/Hydrocarbons Water/Hydrocarbons Water + Hydrocarbons Hydrocarbons Gasoline and Liquefied Petroleum Gas (LPG)
8
Block Flow Diagram Methanol Reactor CO H2H2 MeOH H 2, CO Cooling and Separation MeOH H 2, CO Methanol to Gasoline (MTG) Reactors Water Separation Hydrocarbons Water Hydrocarbons Deethanizer (Dist. Col.) C1/C2 Distillation Columns Heavy Hydrocarbons Liquefied Petroleum Gas Gasoline Purge
9
Methanol Reactor Cooling and Separation T (518F) P (725psi) CO 15,967 lbmol/hr H2 31,935 lbmol/hr T (518F) P (725psi) CO 23,059 lbmol/hr H2 58,373 lbmol/hr MeOH 15,948 lbmol/hr T (345F) P (725psi) CO 22,464 lbmol/hr H2 57,182 lbmol/hr MeOH 576 lbmol/hr T (518F) P (725psi) CO 23,059 lbmol/hr H2 58,373 lbmol/hr MeOH 15,948 lbmol/hr T (364F) P (435psi) T (364F) P (435psi) MeOH 5 lbmol/hr CO 136 lbmol/hr H2 23 lbmol/hr Rec Syngas Syngas Syngas & MeOH Syngas MeOH
10
Methanol to Gasoline (MTG) Reactors Water Separation T (716F) P (362psi) H2O 15,111 lbmol/hr L.G(C1,C2) 211.8 lbmol/hr LPG(C3,C4) 792.5 lbmol/hr C5+(gasoline)2290.8 lbmol/hr MeOH 5 lbmol/hr T (364F) P (435psi) H2O 15,109 lbmol/hr T (305F) P (72psi) H2O 2 lbmol/hr L.G(C1,C2) 211.8 lbmol/hr LPG(C3,C4) 792.5 lbmol/hr C5+(gasoline)2290.8 lbmol/hr T (68F) P (391psi) MeOH Hydrocarbons/ Water Water Hydrocarbons
11
Deethanizer (Dist. Col.) Distillation Columns H2O 2 lbmol/hr L.G(C1,C2) 211.8 lbmol/hr LPG(C3,C4) 792.5 lbmol/hr C5+(gasoline)2290.8 lbmol/hr L.G(C1,C2) 209.2 lbmol/hr LPG(C3,C4) 121.5 lbmol/hr C5+(gasoline) 0.02 lbmol/hr H2O 2 lbmol/hr LPG(C3,C4) 670 lbmol/hr C5+(gasoline)2290.1 lbmol/hr T (68F) P (391psi) T (71F) P (391psi) T (365F) P (363psi) H2O 1.3 lbmol/hr LPG(C3,C4) 663 lbmol/hr C5+(gasoline)485 lbmol/hr H2O 0.30 lbmol/hr LPG(C3,C4) 7.6 lbmol/hr C5+(gasoline)1,805 lbmol/hr T (101F) P (96psi) T (77F) P (73psi) GasolineLPG C1/C2 Heavy Hydrocarbons
12
Design Basis 6000 Short tons syngas/day 518 °F (270 °C) 725 psi (5 Mpa) Product Gasoline – 15,974 barrels/day LPG – 4,263 barrels/day
13
MTG Reactor Sizing 10 Ft/Sec
14
General Plant Layout
15
Site Plan
16
Process Building
17
Economics Capital Cost = $374 Million Syngas cost = $250/ton Gasoline Sold at $2.75 / gallon LPG sold at $1.00 / gallon Plant is profitable 30% IRR $1.473 billion NPV $104 Million in profit / year
18
Gasoline Price Dependence
19
Future of the Mobil Process Coal to gasoline Plants are starting to be built Primus Green – Pennsylvania Biomass to Gasoline South Dakota – New plant in 2012
20
Process Overview 6000 Short Tons / Day Syngas Feed Gasoline- 15,974 barrels/day @ $2.75/gal LPG – 4,263 barrels/day @ $1.00/gal Newton County, Indiana Adjacent to Gasification Plant Plant is profitable Capital Cost = $374 Million Syngas cost = $250/ton 30% IRR $1.473 billion NPV $104 Million in profit / year
21
Conclusions & Further Improvements Further Improvements Reacting out Durene to increase gasoline quality. Alkylation of C4 olefins. Air coolers to reduce cooling water loads. New methods of catalyst regeneration for ZSM-5. Different distillation column set-ups. Pinch analysis for the process. Durene
22
Questions From Last Presentation Our catalyst regeneration for the MTG results in higher alcohols. Is this okay? Yes, they will also be converted to gasoline components You should decouple the reboiler heat duty from the flow of the feed to the distillation columns We will be using bias control
23
Important References Phillips, S. D., Tarud, J. K., Biddy, M. J., & Dutta, A. (2010, January). Gasoline from Wood via integrated gasification, synthesis and methanol to gasoline technology. Retrieved from nrel.gov: http://www.nrel.gov/docs/fy11osti/47594.pdf http://www.nrel.gov/docs/fy11osti/47594.pdf (1994). Kirk-Othmer Encyclopedia of Chemical Technology. In Volume 22 (pp. p 166-168). Exxon Mobil Research and Engineering. (2009). Methanol to Gasoline: Production of clean gasoline from coal. Kooy, P., & Kirk, D. C. (n.d.). The production of methanol and gasoline. Retrieved from http://nzic.org.nz/ChemProcesses/energy/7D.pdf Questions?
Similar presentations
© 2025 SlidePlayer.com. Inc.
All rights reserved.