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The present invention includes Fischer-Tropsch catalysts, reactions using Fischer-Tropsch catalysts, methods of making Fischer-Tropsch catalysts, processes of hydrogenating carbon monoxide, and fuels made using these processes. The invention provides the ability to hydrogenate carbon monoxide with l

The present invention includes Fischer-Tropsch catalysts, reactions using Fischer-Tropsch catalysts, methods of making Fischer-Tropsch catalysts, processes of hydrogenating carbon monoxide, and fuels made using these processes. The invention provides the ability to hydrogenate carbon monoxide with low contact times, good conversion rates and low methane selectivities. In a preferred method, the catalyst is made using a metal foam support.

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We claim: 1. A process for hydrogenating carbon monoxide comprising passing H2 and CO into a reaction chamber comprising a catalyst comprising: a porous support; an interfacial layer; and a Fischer-Tropsch catalytic metal; wherein the catalyst possesses catalytic activity defined by a test in wh

We claim: 1. A process for hydrogenating carbon monoxide comprising passing H2 and CO into a reaction chamber comprising a catalyst comprising: a porous support; an interfacial layer; and a Fischer-Tropsch catalytic metal; wherein the catalyst possesses catalytic activity defined by a test in which the catalyst is placed in a tube inside an isothermal furnace and exposed to a feed stream consisting of a 3 to 1 ratio of hydrogen gas to carbon monoxide, at 250째 C. and a average residence time of 12.5 seconds, the selectivity to methane is greater and the conversion of carbon monoxide is lower at 24 atmospheres than it is at 6 atmospheres of pressure. 2. A process for hydrogenating carbon monoxide, comprising: passing a feed stream comprising hydrogen and carbon monoxide into a reaction chamber containing a catalyst at a temperature of at least 200째 C.; said catalyst comprising a supported Fischer-Tropsch catalytic metal; transferring heat from said reaction chamber to a cooling chamber that is in thermal contact with said reaction chamber, wherein the reaction chamber has a thickness about 1.5 cm or less, at a sufficient rate such that, under steady-state conditions, the feed stream has a contact time of less than about 2 seconds; collecting a product stream; and wherein said process has: a methane selectivity of less than 25%, a carbon monoxide conversion greater than 25%, and a production rate comprising: at least 1 milliliter per minute of liquid product where the volume of liquid product is measured at 20째 C. and 1 atm, or at least 1 liter per minute of gaseous hydrocarbon product wherein the product contains at least 2 carbon atoms per molecule and where the volume of gaseous product is measured at 20째 C. and 1 atm. 3. The process of claim 1 wherein the porous support is metal. 4. The process of claim 1 wherein the catalyst comprises a monolith having a catalyst layer that is less than 20 μm thick. 5. The process of claim 2 wherein the catalyst comprises a metallic porous support. 6. The process of claim 2 wherein the catalyst comprises a monolith having a catalyst layer that is less than 20 μm thick. 7. The process of claim 5 wherein the catalyst comprises a monolith having a catalyst layer that is less than 20 μm thick. 8. The process of claim 5 wherein the catalyst has a porosity of 30 to 99%. 9. The process of claim 8 wherein the catalyst has large pores between about 10 to 300 μm. 10. The process of claim 5 wherein the porous support is selected from the group consisting of foams, felts, wads, and combinations thereof. 11. The process of claim 2 wherein the catalyst is a single piece of contiguous material with contiguous porosity. 12. The process of claim 5 wherein the catalyst has a thickness in the direction of heat transfer of less than 1.5 cm. 13. The process of claim 2 wherein the catalyst has a thickness in the direction of heat transfer of about 1 to about 10 mm. 14. The process of claim 2 wherein a reaction chamber wall separates the reaction chamber from at least one cooling chamber; and further comprising microchannels on the reaction chamber wall separating the reaction chamber from at least one cooling chamber, on the side of the reaction channel wall opposite the catalyst. 15. The process of claim 2 wherein the H2:CO ratio is from about 2:1 to about 3.5:1. 16. The process of claim 15 wherein the temperature is in the range from 200 to 270째 C. 17. The process of claim 12 wherein the contact time is between about 0.1and 1 s. 18. The process of claim 12 wherein the CO conversion is at least 50%. 19. The process of claim 2 wherein the methane selectivity is between about 15% and about 5%. 20. The process of claim 17 wherein the pressure drop through the reaction chamber is less than about 10 psig. 21. The process of claim 19 wherein the pressure drop through the reaction chamber is less than about 15 psig. 22. The process of claim 20 wherein the CO conversion is greater than about 80%. 23. The process of claim 17 wherein the catalyst has a thickness in the direction of heat transfer of about 1 to about 3 mm. 24. The process of claim 14 wherein the catalyst has a thickness in the direction of heat transfer of less than 1.5 cm. 25. The process of claim 24 wherein the catalyst has a thickness in the direction of heat transfer of about 3 mm or less. 26. The process of claim 2 wherein a reaction chamber wall separates the reaction chamber from at least one cooling chamber; and further wherein the reaction chamber comprises a microchannel. 27. The process of claim 26 wherein the contact time is less than 2 seconds, methane selectivity is less than 20%, and the CO conversion is at least 50%. 28. The process of claim 26 wherein the contact time is between about 0.1 and 1 second, and CO conversion is greater than 80%. 29. The process of claim 26 wherein the methane selectivity is between about 15% and 5%. 30. The process of claim 26 wherein the catalyst comprises a porous support. 31. The process of claim 28 wherein the catalyst comprises a metallic porous support.