用于反向水煤气转换催化剂和集成费-托工艺的镍催化剂

  We Claim : 1. A method for performing a reverse water-gas shift reaction, the method comprising : contacting at a temperature in the range of 500-900 °C a supported reverse water- gas shift catalyst with a feed stream comprising CO2 and H2, to provide a product stream comprising CO and H2, the product stream having a lower concentration of CO2 and a higher concentration of CO than the feed stream; wherein the catalyst comprises : a support that is a cerium oxide support, a titanium oxide support, an aluminum oxide support, a zirconium oxide support, or a mixed oxide support comprising a mixture of two or more of cerium oxide, titanium oxide, aluminum oxide, and zirconium oxide; nickel, present in an amount in the range of 0.05 to 10 wt% of the catalyst, based on the total weight of the catalyst; and manganese, present in an amount in the range of 0.5 to 20 wt% of the catalyst, based on the total weight of the catalyst. 2. The method of claim 1, wherein the reverse water-gas shift reaction has a CO selectivity of at least 50%. 3. The method of claim 1, wherein the reverse water-gas shift reaction has a methane selectivity of no more than 40%. 4. The method of claim 1, having a CO2 conversion of at least 30%. 5. The method of claim 1, having a CO2 conversion of no more than 90%. 6. The method of claim 1, conducted at a temperature in the range of 600-800 °C. 7. The method of claim 1, wherein the molar ratio of H2 to CO2 in the feed stream is in the range of 0.5 : 1 to 10 : 1. 8. The method of claim 1, wherein the product stream comprises no more than 75 mol% CO2.     9. The method of claim 1, wherein the product stream further comprises CO2, and wherein the method further comprises recycling at least a portion of the CO2 of the product stream to the feed stream. 10. The method of claim 1, wherein the product stream further comprises hydrogen and wherein the method further comprises recycling at least a portion of the hydrogen of the product stream to the feed stream. 11. The method of claim 1, wherein the product stream comprises no more than 40 mol% methane. 12. The method of claim 1, wherein the product stream comprises no more than 10 mol% methane. 13. A process for performing an integrated Fischer-Tropsch process, the process comprising : providing a first feed stream comprising H2 and CO2; contacting at a first temperature in the range of 500-900 °C and at a first pressure a reverse water-gas shift catalyst with the first feed stream to perform a reverse water-gas shift reaction to provide a first product stream comprising CO and H2, the first product stream having a lower concentration of CO2 and a higher concentration of CO than the first feed stream; contacting at a second temperature and at a second pressure a Fischer-Tropsch catalyst with a second feed stream comprising H2 and at least a portion of CO of the first product stream to provide a second product stream comprising C5+ hydrocarbons, wherein the reverse water-gas shift catalyst is a supported reverse water-gas shift catalyst comprising : a support that is a cerium oxide support, a titanium oxide support, an aluminum oxide support, a zirconium oxide support, or a mixed oxide support comprising a mixture of two or more of cerium oxide, titanium oxide, aluminum oxide, and zirconium oxide; nickel, present in an amount in the range of 0.05 to 10 wt% of the catalyst, based on the total weight of the catalyst; and manganese, present in an amount in the range of 0.5 to 20 wt% of the catalyst, based on the total weight of the catalyst.     14. The process of claim 13, wherein the support makes up at least 70 wt% of the catalyst, on an oxide basis. 15. The process of claim 13, wherein nickel is present in the catalyst in an amount in the range of 0.1 to 10 wt%. 16. The process of claim 13, wherein manganese is present in the catalyst in an amount in the range of 2 to 20 wt%. 17. The process of claim 13, wherein a ratio of nickel to manganese is in the range of 0.05 : 1 to 1 : 1. 18. The process of claim 13, wherein the molar ratio of H2 to CO2 in the first feed stream is in the range of 0.5 : 1 to 10 : 1. 19. The process of claim 13, wherein the reverse water-gas shift reaction has a methane selectivity of no more than 10%. 20. The process of claim 13, wherein the process comprises activating the reverse water-gas shift catalyst with a reducing stream comprising a reductive gas. 21. The process of claim 13, wherein the first product stream comprises no more than 75 mol% CO2. 22. The process of claim 13, wherein the first product stream comprises no more than 40 mol% methane. 23. The process of claim 13, wherein at least 25% of the CO of the first product stream is included in the second feed stream. 24.  The process of claim 13, wherein the first product stream includes H2, and wherein at least 25% of the H2 of the first product stream is included in the second feed stream. 25. The process of claim 13, wherein at least 10% of the CO2 of the first product stream is included in the second feed stream.     26. The process of claim 13, wherein the second feed stream does not include a substantial amount of CO2 of the first product stream. 27. The process of claim 13, wherein the second feed stream has a H2 : CO ratio in the range of 0.5 : 1 to 6 : 1. 28. The process of claim 13, wherein the second temperature is in the range of 200-350 °C. 29. The process of claim 13, wherein the first temperature is at least 100 °C greater than the second temperature than the second temperature. 30. The process of claim 13, wherein the contacting of the Fischer-Tropsch catalyst with the second feed stream to provide the second product stream is performed with a selectivity for C5+ alkanes of at least 30%. 31. The process of claim 13, further comprising separating at least a portion of C1-C4 hydrocarbons from the second product stream to provide a light hydrocarbon stream. 32. The process of claim 13, wherein the process further comprises exchanging heat between at least a portion of the second product stream and at least a portion of the second feed stream, thereby cooling at least a portion of the second product stream and heating at least a portion of the second feed stream. 33.  The process of claim 13, further comprising recycling at least a portion of H2 of the second product stream to the second feed stream. 34. The process of claim 13, further comprising recycling at least a portion of H2 of the second product stream to the first feed stream, wherein H2 from the second product stream makes up at least 90% of the H2 of the first feed stream. 35. The process of claim 13, further comprising recycling at least a portion of CO of the second product stream to the second feed stream or the first feed stream. 36. The process of claim 13, further comprising recycling at least a portion of CO2 of the second product stream to the first feed stream, wherein CO2 from the second product stream makes up at least 90% of the CO2 of the first feed stream.     37. A supported reverse water-gas shift catalyst comprising : a support that is a cerium oxide support, a titanium oxide support, an aluminum oxide support, a zirconium oxide support, or a mixed oxide support comprising a mixture of two or more of cerium oxide, titanium oxide, aluminum oxide, and zirconium oxide; nickel, present in an amount in the range of 0.05 to 10 wt% of the catalyst, based on the total weight of the catalyst; and manganese, present in an amount in the range of 0.5 to 20 wt% of the catalyst, based on the total weight of the catalyst. 38. The catalyst of claim 37, wherein at least a surface layer of the cerium oxide support comprises at least 90 wt% cerium oxide, e.g., at least 95 wt% cerium oxide, or at least 98 wt% cerium oxide, on an oxide basis. 39. The catalyst of claim 37, wherein the total amount of cerium, titanium, aluminum, zirconium, manganese, and nickel in the catalyst is at least 90 wt%, e.g., at least 95 wt% or at least 98 wt% of the catalyst, on a metallic basis.