초록 ▼

The disclosed invention relates to a process and apparatus for converting natural gas to higher molecular weight hydrocarbons. The process includes steam reforming to form synthesis gas followed by a Fischer-Tropsch reaction to convert the synthesis gas to the high molecular weight hydrocarbons. The

The disclosed invention relates to a process and apparatus for converting natural gas to higher molecular weight hydrocarbons. The process includes steam reforming to form synthesis gas followed by a Fischer-Tropsch reaction to convert the synthesis gas to the high molecular weight hydrocarbons. The reforming and Fischer-Tropsch reactions are conducted in microchannel reactors. The higher molecular weight hydrocarbons may be further treated to form hydrocarbon products such as middle distillate fuels, lubricating oils, and the like. The apparatus includes vessels containing SMR microchannel reactors and Fischer-Tropsch microchannel reactors. A composition comprising a mixture of olefins and paraffins is disclosed.

대표청구항 ▼

The invention claimed is: 1. A process, comprising: (A) flowing an SMR feed in an SMR microchannel reactor in contact with one or more SMR catalysts to form a first intermediate product, the SMR feed comprising methane and steam, the first intermediate product comprising CO and H2; the SMR microcha

The invention claimed is: 1. A process, comprising: (A) flowing an SMR feed in an SMR microchannel reactor in contact with one or more SMR catalysts to form a first intermediate product, the SMR feed comprising methane and steam, the first intermediate product comprising CO and H2; the SMR microchannel reactor comprising a plurality of SMR process microchannels and a plurality of combustion channels; the SMR process microchannels containing the one or more SMR catalysts, the methane and steam contacting the one or more SMR catalysts in the process microchannels; separating part of the H2 from the first intermediate product to form a second intermediate product, the second intermediate product comprising CO and H2; the combustion channels containing one or more combustion catalysts, the separated H2 being combined with oxygen or a source of oxygen to form a combustion reaction mixture; the combustion reaction mixture contacting the one or more combustion catalysts, undergoing a combustion reaction, and generating heat and a combustion exhaust; transferring heat from the combustion channels to the SMR process microchannels; and (B) flowing the second intermediate product in a Fischer-Tropsch microchannel reactor in contact with one or more Fischer-Tropsch catalysts to form a Fischer-Tropsch product comprising one or more higher molecular weight hydrocarbons; the Fischer-Tropsch microchannel reactor comprising a plurality of Fischer-Tropsch process microchannels and a plurality of heat exchange channels; the Fischer-Tropsch process microchannels containing the one or more Fischer-Tropsch catalysts, the second intermediate product contacting the one or more Fischer-Tropsch catalysts in the Fischer-Tropsch process microchannels; transferring heat from the Fischer-Tropsch process microchannels to a heat exchange fluid in the heat exchange channels. 2. The process of claim 1 wherein the Fischer-Tropsch product formed in step (B) further comprises a gaseous mixture comprising CO and H2, the gaseous mixture being separated from the Fischer-Tropsch product, the separated gaseous mixture comprising a third intermediate product, the process further comprising: (C) flowing the third intermediate product in a second Fischer-Tropsch microchannel reactor in contact with one or more second Fischer-Tropsch catalysts to form a second Fischer-Tropsch product comprising one or more higher molecular weight hydrocarbons; the second Fischer-Tropsch microchannel reactor comprising a plurality of second Fischer-Tropsch process microchannels and a plurality of second heat exchange channels; the second Fischer-Tropsch process microchannels containing one or more second Fischer-Tropsch catalysts, the third intermediate product contacting the one or more second Fischer-Tropsch catalysts in the second Fischer-Tropsch process microchannels; transferring heat from the second Fischer-Tropsch process microchannels to a heat exchange fluid in the second heat exchange channels. 3. The process of claim 1 wherein the SMR feed is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor, at least part of the tail gas being combined with the natural gas feed. 4. The process of claim 1 wherein the SMR feed is derived from a natural gas feed, and process water is formed in the Fischer-Tropsch microchannel reactor, at least a portion of the process water being combined with the natural gas feed. 5. The process of claim 1 wherein the SMR feed is derived from a natural gas feed, and process water is formed in the Fischer-Tropsch microchannel reactor and is combined with the natural gas feed, and tail gas is formed in the Fischer-Tropsch microchannel reactor and at least part of the tail gas is combined with the natural gas feed. 6. The process of claim 5 wherein the natural gas feed, process water and tail gas are combined in a saturator, the saturator being upstream of the SMR microchannel reactor. 7. The process of claim 1 wherein the SMR feed comprises one or more higher molecular weight hydrocarbons, the process further comprising flowing the SMR feed and steam in a pre-reformer to convert at least some of the higher molecular weight hydrocarbons in the SMR feed to methane, the pre-reformer being upstream of the SMR microchannel reactor. 8. The process of claim 1 wherein the SMR feed comprises one or more higher molecular weight hydrocarbons, the process further comprising flowing the SMR feed and steam in a pre-reformer to convert at least some of the higher molecular weight hydrocarbons in the SMR feed to methane, the pre-reformer being integrated with the SMR microchannel reactor and being heated by heat from the combustion channels. 9. The process of claim 1 wherein the SMR feed comprises one or more higher molecular weight hydrocarbons, the process further comprising flowing the SMR feed and steam in the SMR process microchannels at a first temperature in a first part of the SMR process microchannels to convert at least some of the higher molecular weight hydrocarbons in the SMR feed to methane, the resulting product comprising a modified SMR feed comprising methane, and flowing the modified SMR feed in a second part of the SMR process microchannels at a second temperature to convert the modified SMR feed to the first intermediate product. 10. The process of claim 1 wherein staged addition channels are positioned adjacent to the combustion channels, the oxygen source of oxygen flowing through to the staged addition channels into the combustion channels. 11. The process of claim 1 wherein the combustion exhaust comprises a vapor and a liquid, the vapor being separated from the liquid in a vapor-liquid separator, the liquid comprising water. 12. The process of claim 1 wherein the SMR feed is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor, the tail gas comprising H2, CO, CO2 and one or more hydrocarbons, the tail gas flowing through an H2 separator to provide a carbon rich tail gas and an H2 rich tail gas, the carbon rich tail gas being combined with the natural gas feed, the H2 rich tail gas being used as a fuel. 13. The process of claim 1 wherein a tail gas is formed in the Fischer-Tropsch microchannel reactor, the tail gas comprising N2, the tail gas flowing through a nitrogen separator wherein N2 is separated from the tail gas. 14. The process of claim 1 wherein the SMR feed is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor, the tail gas comprising H2, N2, CO, CO2 and one or more hydrocarbons, the tail gas flowing through an H2 separator to provide a carbon rich tail gas and an H2 rich tail gas, the carbon rich tail gas comprising N2, the carbon rich tail gas flowing through a nitrogen separator wherein N2 is separated from the carbon rich tail gas, the carbon rich tail gas being combined with the natural gas feed, the H2 rich tail gas being used as a fuel. 15. The process of claim 1 wherein the second intermediate product is compressed prior to step (B). 16. The process of claim 1 wherein the SMR feed is derived from a natural gas feed, and a tail gas is formed in the Fischer-Tropsch microchannel reactor and at least part of the tail gas is combined with the natural gas feed, the at least part of the tail gas being compressed prior to being combined with the natural gas feed. 17. The process of claim 1 wherein the heat exchange fluid in the heat exchange channels is at least partially vaporized in the heat exchange channels. 18. The process of claim 1 wherein the Fischer-Tropsch product comprises one or more paraffins and/or one or more olefins of about 5 to about 100 carbon atoms. 19. The process of claim 1 wherein the Fischer-Tropsch product comprises olefins and paraffins, the ratio of olefins to paraffins being in the range from about 0.01 to about 0.8. 20. The process of claim 1 wherein the Fischer-Tropsch product is further processed using hydrocracking, hydroisomerizing or dewaxing. 21. The process of claim 1 wherein natural gas is used in the formation of the SMR feed, the percent of carbon in the Fischer-Tropsch product relative to carbon in the natural gas being in the range from about 50 to about 70%. 22. The process ofclaim 2 wherein natural gas is used in the formation of the SMR feed, the overall percent of carbon in the first and second Fischer-Tropsch products relative to carbon in the natural gas is at least about 75%. 23. The process of claim 1 wherein each SMR process microchannel has at least one heat transfer wall and the heat flux for heat exchange within the SMR microchannel reactor is in the range from about 0.01 to about 500 watts per square centimeter of surface area of the heat transfer walls. 24. The process of claim 1 wherein each SMR process microchannel has a first part wherein the temperature is in the range from about 150 to about 400° C., and a second part downstream of the first part wherein the temperature is in the range from about 600 to about 1000° C. 25. The process of claim 1 wherein each Fischer-Tropsch process microchannel has at least one heat transfer wall and the heat flux for heat exchange within the Fischer-Tropsch microchannel reactor is in the range from about 0.01 to about 500 watts per square centimeter of surface area of the heat transfer walls. 26. The process of claim 1 wherein one or more multi-stream heat exchangers provide for exchange of heat between the SMR feed and first intermediate product, and between the H2 and the oxygen or source of oxygen of the combustion reaction mixture and the combustion exhaust. 27. The process of claim 1 wherein H2 is separated from the first intermediate product using temperature swing adsorption, pressure swing adsorption, membranes, or a combination of two or more thereof. 28. The process of claim 12 wherein temperature swing adsorption, pressure swing adsorption, membranes, or a combination of two or more thereof, is used to separate the carbon rich tail gas from the H2 rich tail gas. 29. The process of claim 13 wherein temperature swing adsorption, pressure swing adsorption, membranes, or a combination of two or more thereof, is used to separate the N2 from the tail gas. 30. The process of claim 14 wherein temperature swing adsorption, pressure swing adsorption, membranes, or a combination of two or more thereof, is used to separate H2 from the tail gas and to separate N2 from the carbon rich tail gas. 31. The process of claim 1 wherein the SMR catalyst comprises La, Pt, Fe, Ni, Ru, Rh, In, Ir, W, and/or an oxide thereof, or a mixture of two or more thereof. 32. The process of claim 31 wherein the SMR catalyst further comprises MgO, Al2O3, SiO2, TiO2, or a mixture of two or more thereof. 33. The process of claim 1 wherein the combustion catalyst comprises Pd, Pr, Pt, Rh, Ni, Cu, and/or an oxide thereof, or a mixture of two or more thereof. 34. The process of claim 33 wherein the combustion catalyst further comprises Al2O3, SiO2, MgO, or a mixture of two or more thereof. 35. The process of claim 1 wherein the Fischer-Tropsch catalyst comprises one or more of Co, Fe, Ni, Ru, Re, Os, and/or an oxide thereof, or a mixture of two or more thereof. 36. The process of claim 1 wherein the Fischer-Tropsch catalyst comprises one or more metals from Group IA, IIA, IIIB or IIIB of the Periodic Table and/or an oxide thereof, a lanthanide metal and/or oxide thereof, an actinide metal and/or oxide thereof, or a mixture of two or more thereof. 37. The process of claim 1 wherein the SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is in the form of particulate solids. 38. The process of claim 1 wherein the SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is coated on interior walls of the channels, grown on interior walls of the channels, or coated on a fin structure. 39. The process of claim 1 wherein the SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is supported on a support structure having a flow-by configuration, a flow-through configuration, or a serpentine configuration. 40. The process of claim 1 wherein the SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is supported on a support structure having the configuration of a foam, felt, wad, fin, or a combination of two or more thereof. 41. The process of claim 1 wherein the SMR catalyst, combustion catalyst and/or Fischer-Tropsch catalyst is supported on a support structure in the form of a fin assembly comprising at least one fin. 42. A process, comprising: (A) flowing an SMR feed in an SMR microchannel reactor in contact with one or more SMR catalysts to form a first intermediate product, the SMR feed comprising methane and steam, the first intermediate product comprising CO and H2; the SMR microchannel reactor comprising a plurality of SMR process microchannels and a plurality of combustion channels; the SMR process microchannels containing the one or more SMR catalysts, the methane and steam contacting the one or more SMR catalysts in the process microchannels; separating part of the H2 from the first intermediate product to form a second intermediate product, the second intermediate product comprising CO and H2; the combustion channels containing one or more combustion catalysts, the separated H2 being combined with oxygen or a source of oxygen to form a combustion reaction mixture; the combustion reaction mixture contacting the one or more combustion catalysts, undergoing a combustion reaction, and generating heat and a combustion exhaust; transferring heat from the combustion channels to the SMR process microchannels; (B) flowing the second intermediate product in a Fischer-Tropsch microchannel reactor in contact with one or more Fischer-Tropsch catalysts to form a Fischer-Tropsch product comprising one or more higher molecular weight hydrocarbons, and a gaseous mixture comprising CO and H2; the Fischer-Tropsch microchannel reactor comprising a plurality of Fischer-Tropsch process microchannels and a plurality of heat exchange channels; the Fischer-Tropsch process microchannels containing the one or more Fischer-Tropsch catalysts, the second intermediate product contacting the one or more Fischer-Tropsch catalysts in the Fischer-Tropsch process microchannels; separating the gaseous mixture from the Fischer-Tropsch product, the separated gaseous mixture comprising a third intermediate product; transferring heat from the Fischer-Tropsch process microchannels to a heat exchange fluid in the heat exchange channels; and (C) flowing the third intermediate product in a second Fischer-Tropsch microchannel reactor in contact with one or more second Fischer-Tropsch catalysts to form a second Fischer-Tropsch product comprising one or more higher molecular weight hydrocarbons; the second Fischer-Tropsch microchannel reactor comprising a plurality of second Fischer-Tropsch process microchannels and a plurality of second heat exchange channels; the second Fischer-Tropsch process microchannels containing one or more second Fischer-Tropsch catalysts, the third intermediate product contacting the one or more second Fischer-Tropsch catalysts in the second Fischer-Tropsch process microchannels; transferring heat from the second Fischer-Tropsch process microchannels to a heat exchange fluid in the second heat exchange channels. 43. The process ofclaim 1 wherein the Fischer-Tropsch product is hydrocracked in a hydrocracker operated in series with the Fischer-Tropsch microchannel reactor.