1. XtL – the Topsøe Approach

2. 2 Presentation outline  General introduction –Haldor Topsøe –What is XtL? –Focus of this presentation  Building blocks –Gasification –Sour gas shift –Gas purification including Acid Gas Removal (AGR) –Downstream synthesis  TIGAS  Conclusions

3. 3 Haldor Topsøe A/S Year of establishment: 1940; Incorporated: 1972 Ownership: Haldor Topsøe Holding A/S (100%) Subsidiaries:  Haldor Topsoe, Inc.  Haldor Topsøe International A/S, Denmark –Haldor Topsoe India Pvt. Ltd. India  ZAO Haldor Topsøe, Russia  Topsoe Fuel Cell A/S, Denmark Annual turnover (2009):  > 4.25 billion DKK (~572 MM EUR)  Number of employees (2009): ~2100

4. 4 Offices worldwide Headquarters City of Topsøe office Research Production Engineering Sale & Marketing Copenhagen Moscow Beijing Tokyo Bahrain New Delhi Buenos Aires Los Angeles Houston Edmonton

5. 5 Topsøe is dedicated to…  Research and development in heterogeneous catalysis  Production and sale of catalysts  Licensing of technology  Equipment supply  Engineering and construction of plants based on catalytic processes

6. 6 Business areas  Fertiliser industry  The heavy chemical and petrochemical industries  The refining industry  The environmental and power sector

7. 7 What is XtL?  Any feedstock (bio, coal, natural gas) for production of liquid products  Relatively well-known building blocks  Challenges within –Gasifier characteristics –Gas conditioning –Selection of Acid Gas Removal (AGR)  Integration with downstream synthesis

8. 8 Topsøe XtL technologies  Ammonia  Methanol  DME  Gasoline - TIGAS  Higher alcohols 34,000 bbl/d GTL plant 2100 TPD ammonia plant

9. 9 A simple block diagram

10. 10 Focus of this presentation  Describing the route from coal gas to gasoline via Topsøe’s TIGAS process  Many other end products exist, but time limits description of alternatives

11. 11 Building blocks  Gasification  Sour gas shift  Gas purification including Acid Gas Removal (AGR)  Downstream synthesis

12. 12 Coal gas conditioning Air Separation unit Air Separation unit Gasification Sour Water Gas Shift Acid Gas Removal Acid Gas Removal Sulfur Recovery (WSA) Sulfur Recovery (WSA) Final Gas Purification Final Gas Purification O2O2 CO 2 CO 2 / H 2 S Sulphuric acid Air H2OH2O Synthesis gas Coal H 2 /CO = 1 ( TIGAS/DME ) H 2 /CO = 2 ( MeOH/FT ) H 2 /CO = 3 (SNG ) H 2 /CO = ∞ ( H 2, NH 3 )

13. 13 Gasification CO H 2 CO 2 Coal Biomass Hydrogen Ammonia Methanol DME Gasoline Diesel SNG Synthesis Gas 20-70 bar 900-1500°C

14. 14

15. 15 Sour shift  Module (H 2 /CO) adjustment  CO + H 2 O ↔ CO 2 + H 2  Extent of shift depending on gasifier and synthesis  H 2 S in raw feed gas  Low steam to dry gas ratio preferred –Low CO 2 emission –Higher efficiency

16. 16 Gas purification  Catalyst poison removal –Arsenic –Chlorine –H 2 S –COS –Organic sulphur –Etc.  ppb & ppm reactions Pure syngas << 10 ppb sulphur! Syngas from CO 2 -removal

17. TIGAS – from natural gas, coal, biomass or waste to clean transportation fuels

18. 18 TIGAS - History  Houston demonstration in mid 80-ies  Mobil’s MTG in New Zealand (1984-1995)  Crude oil price development caused a ‘cooled-down’ interest in synthetic gasoline  Renewed interest in MTG and TIGAS (~ 2005)  One plant in China started up (2009) based on ExxonMobil’s MTG  TIGAS granted DOE funding (25 million USD) in 2009 – bio feedstock

19. 19 Gasoline C 3 -C 4 Water Gasoline synthesis Separation Off-gas MeOH/DME synthesis Synthesis gas CO 2 removal CO 2 LOW RECYCLE RATE ( R/ M < 1 ) REDUCED STEAM CONSUMPTION (LESS MODULE ADJUSTMENT) ”DRY” FEED (low P H2O ) LESS PROCESS CONDENSATE IMPROVED CONVERSION Coal gas to gasoline

20. 20 Methanol to gasoline SynGas  MeOH ; MeOH  DME  Gasoline S y nGas  MeOH/DME  Gasoline MTG ( M ethanol T o G asoline) 15,000 bbl/d Industrial Plant, Motonui, NZ TIGAS ( T opsøe I ntegrated GA soline S ynthesis) > 20,000 hrs. Pilot Plant Operation Mobil (MTG): Topsøe (TIGAS):

21. 21 Methanol synthesis Gasoline C 3 -C 4 Water MTG Methanol To Gasoline MeOH↔DME Gasoline synthesis Separation Day tank ( raw methanol ) Off-gas Synthesis gas MeOH/DME synthesis TIGAS Topsøe Integrated Gasoline Synthesis Simple process layout No methanol condensation / re-evaporation Low recycle Moderate pressure

22. 22 2H 2 + CO = MeOH 2MeOH = DME + H 2 O CO + H 2 O = CO 2 + H 2 MeOH/DME synthesis (at low H 2 /CO) 3H 2 + 3CO = CH 3 OCH 3 + CO 2

23. 23 ▼ DMEMeOH H2OH2O CO 2 H2H2 CO Recycle H 2 /CO ≈ 1 H 2 /CO = 1 is the optimum for DME (equilibrium) mol-% H 2 /CO  Adjust module by SHIFT inside loop - eliminates the need for upstream module adjustment High conversion makes CO 2 removal inside synthesis loop feasible H 2 /CO < 1 ▼

24. 24 TIGAS - Latest development - Wood to gasoline project, Chicago ~25 million USD funding by DOE O2O2

25. 25 Conclusions  TIGAS is a viable option for XtL  Feedstock flexibility  TIGAS is an interesting option for the utilisation of associated gas  Mix of legislative, economic and political factors as main drivers  Demonstration in Chicago  TIGAS is CCS ready