[특허]Solid/liquid separation system for multiphase converters

ConocoPhillips Company

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Solid/liquid separation system for multiphase converters

특허상세정보
국가/구분	United States(US) Patent 등록
국제특허분류(IPC7판)	B01D-037/02 B01D-037/04
미국특허분류(USC)	210/777; 210/791; 210/193
출원번호	US-0414636 (2003-04-16)
§371/§102 date	20030224 (20030224)
발명자 / 주소	Espinoza, Rafael L. Mohedas, Sergio R. Jack, Doug S. Odueyungbo, Oluwaseyi A. Ortego, Jr., James Dale
출원인 / 주소	ConocoPhillips Company
대리인 / 주소	Conley Rose P.C.
인용정보	피인용 횟수 : 8 인용 특허 : 19

초록
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Methods and apparatus for removing wax products from a slurry used in a Fischer-Tropsch reactor. The preferred embodiments of the present invention are characterized by a solid/liquid separation system that removes liquid products from a slurry by drawing the fluid across a filter medium composed of a filter cake disposed on a substrate. In the preferred embodiments, the filter cake is desirable and performs the majority of the filtration. In certain embodiments, the filter medium is disposed in a filter housing where slurry flows parallel to the longitudinal axis of the filter medium from and inlet to an outlet. The characteristics or properties of the cake, which will effect the performance of the solid/liquid separation system, can be controlled by regulating the velocity of the slurry flowing across the cake, where the velocity may be regulated by adjusting the slurry flow through the filter housing or may be self-regulated by changing slurry velocities influenced by the design of the filter housing.

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1. A method for operating a filtration system comprising:providing a filtration housing comprising a slurry chamber and a filtrate chamber separated by a filter medium, wherein the filter medium comprises a filter cake disposed on a substrate, wherein the filter cake has a thickness and provides a substantial majority of the filtration activity; passing a slurry, comprising a liquid phase and a solid phase, at a slurry linear velocity through the slurry chamber; applying a pressure differential between the slurry chamber and the filtrate chamber in order to permeate a portion of the liquid phase of the slurry through the filter medium, wherein the filter medium's filtrate flux is at least partially dependent on the thickness of the filter cake; and regulating the slurry linear velocity to control the thickness of the filter cake. 2. The method according to claim 1 wherein at least a portion of the filter cake comprises particles from the slurry solid phase.3. The method according to claim 1 wherein the substrate has a nominal rating and a fraction of slurry solid phase comprises particles having a size smaller than the substrate nominal rating.4. The method according to claim 1 wherein at least 95 weight percent of the particles fall within the range 10-200 um.5. The method according to claim 1 wherein the slurry solid phase has a number average particle size between 20 and 50 um.6. The method according to claim 1 wherein the slurry solid phase comprises from 5 to 25 vol % of the slurry.7. The method according to claim 1 wherein the substrate comprises a medium selected from the group consisting of sintered woven wire-mesh media, sintered powered metal media, porous metal fiber, metal supported membranes, and wedged wire media.8. The method according to claim 1 wherein the filtrate medium's filtrate flux is independent of substrate morphology.9. The method according to claim 1 wherein the substrate has a cylindrical body with a longitudinal axis parallel to the direction of the slurry flow through the slurry chamber.10. The method according to claim 1 wherein the slurry linear velocity is less than 5.0 ft/sec.11. The method according to claim 1 wherein the slurry linear velocity is between 0.1 and 5.0 ft/sec.12. The method according to claim 1 wherein the filtration system has a filtration flux of at least 0.2 gal/min/ft2.13. The method according to claim 1 wherein the liquid phase comprises hydrocarbons produced from Fischer-Tropsch synthesis and the solid phase comprises a catalyst active for Fischer-Tropsch synthesis.14. The method according to claim 13 wherein the catalyst comprises at least one of cobalt, ruthenium, or iron.15. The method according to claim 13 wherein the catalyst comprises a support selected from the group consisting of alumina, silica, titania, zirconia, and combinations thereof.16. The method according to claim 1 wherein the pressure differential between the slurry chamber and the filtrate chamber is less than 30 psi.17. The method according to claim 1 wherein the slurry linear velocity is regulated by the volumetric flow rate of the slurry through the filtration housing such that the slurry linear velocity increases as the thickness of the filter cake increases and the slurry linear velocity decreases as the thickness of the filter cake decreases.18. The method of claim 1 wherein the slurry is circulated to and from the filtration system in a circulation loop and the slurry linear velocity is regulated by the configuration of the circulation loop.19. The method of claim 1 wherein the slurry linear velocity is regulated by the design of the filter housing.20. The method of claim 1 wherein the slurry is circulated between a Fischer-Tropsch reactor and the filtration system in a circulation loop and the slurry linear velocity is regulated by varying the gas hold up in the Fischer-Tropsch reactor.21. The method of claim 1 wherein the slurry linear velocity is regulated using valves to control the flow of slurry.22. The method according to claim 1 wherein the slurry linear velocity is regulated by adding a liquid stream to the slurry passing through the slurry chamber.23. A method for operating a filtration system comprising:providing a filtration housing comprising a slurry chamber and a filtrate chamber separated by a substrate; passing a slurry, comprising a liquid phase and a solid phase, through the slurry chamber at a slurry linear velocity; applying a pressure differential between the slurry chamber and the filtrate chamber so as to form a filter cake comprising a portion of the slurry solid phase disposed on the substrate; permeating a portion of the slurry liquid phase through the filter cake and the substrate to generate a filtrate flux, wherein the filter cake acts as a filter such that the filtrate flux is substantially dependent on one or more filter cake properties and independent of the substrate morphology; and regulating the slurry linear velocity through the slurry chamber to control at least one filter cake property. 24. The method according to claim 23 wherein the controlled cake property is cake permeability.25. The method according to claim 23 wherein the controlled cake property is cake thickness.26. The method according to claim 23 wherein the substrate has a nominal rating and a fraction of slurry solid phase comprises particles having a size smaller than the substrate nominal rating.27. The method according to claim 23 wherein at least 95 weight percent of the particles fall within the range 10-200 um.28. The method according to claim 23 wherein the slurry solid phase has a number average particle size between 20 and 50 um.29. The method according to claim 23 wherein the solid phase comprises from 5 to 25 vol % of the slurry.30. The method according to claim 23 wherein the substrate has a cylindrical body with a longitudinal axis parallel to the direction of the slurry flow through the slurry chamber.31. The method according to claim 23 wherein the slurry linear velocity is less than 5.0 ft/sec.32. The method according to claim 23 wherein the slurry linear velocity is between 0.1 and 5.0 ft/sec.33. The method according to claim 23 wherein the filtration system has a filtration flux of at least 0.2 gal/min/ft2.34. The method according to claim 23 wherein the liquid phase comprises hydrocarbons produced from Fischer-Tropsch synthesis and the solid phase comprises a catalyst active for Fischer-Tropsch synthesis.35. The method according to claim 34 wherein the catalyst comprises at least one of cobalt, ruthenium, or iron.36. The method according to claim 34 wherein the catalyst comprises a support selected from the group consisting of alumina, silica, titania, zirconia, and combinations thereof.37. The method according to claim 23 wherein the pressure differential between the slurry chamber and the filtrate chamber is less than 30 psi.38. The method according to claim 23 wherein the slurry linear velocity is regulated by the volumetric flow rate of the slurry through the filtration housing such that the slurry linear velocity increases as the thickness of the filter cake increases and the slurry linear velocity decreases as the thickness of the filter cake decreases.39. The method of claim 23 wherein the slurry is circulated to and from the filtration system in a circulation loop and the slurry linear velocity is regulated by controlling the configuration of the circulation loop.40. The method of claim 23 wherein the slurry linear velocity is regulated by the design of the filter housing.41. The method of claim 23 wherein the slurry is circulated between a Fischer-Tropsch reactor and the filtration system in a circulation loop and the slurry linear velocity is regulated by varying the gas hold up in the Fischer-Tropsch reactor.42. The method of claim 23 wherein the slurry linear velocity is regulated using valves to control the flow of slurry.43. The method according to claim 23 wherein the slurry linear velocity is regulated by adding a liquid stream to the slurry passing through the slurry chamber.44. A method for operating a filtration system comprising steps:a) providing a filtration housing comprising a slurry chamber, a substrate and a filtrate chamber; b) feeding a slurry comprising a liquid phase and a solid phase to the slurry chamber at a slurry linear velocity c) applying a differential pressure between the slurry chamber and the filtrate chamber to form a cake disposed on the substrate, wherein the cake at least partially comprises particles from the slurry solid phase disposed on the substrate and wherein the cake provides a substantial majority of the filtration activity; d) permeating a portion of the slurry liquid phase through the cake and the substrate to generate a filtrate flux that is substantially independent of the substrate morphology; e) intermittently ceasing at least steps c & d in order to remove at least a portion of the cake from the substrate and then resuming c & d. 45. The method according to claim 44 wherein at least a portion of the cake is removed by reversing the filtrate flow across the substrate or passing a gas stream from the filtrate chamber to the slurry chamber.46. The method according to claim 44 wherein the controlled cake property is cake permeability.47. The method according to claim 44 wherein the controlled cake property is cake thickness.48. The method according to claim 44 wherein the substrate has a nominal rating and a fraction of slurry solid phase comprises particles having a size smaller than the substrate nominal rating.49. The method according to claim 44 wherein at least 95 weight percent of the particles fall within the range 10-200 um.50. The method according to claim 44 wherein the slurry solid phase has a number average particle size between 20 and 50 um.51. The method according to claim 44 wherein the solid phase comprises from 5 to 25 vol % of the slurry.52. The method according to claim 44 wherein the substrate has a cylindrical body with a longitudinal axis parallel to the direction of the slurry flow through the slurry chamber.53. The method according to claim 44 wherein the slurry linear velocity is less than 5.0 ft/sec.54. The method according to claim 44 wherein the slurry linear velocity is between 0.1 and 5.0 ft/sec.55. The method according to claim 44 wherein the filtration system has a filtration flux of at least 0.2 gal/min/ft2.56. The method according to claim 44 wherein the liquid phase comprises hydrocarbons produced from Fischer-Tropsch synthesis and the solid phase comprises a catalyst active for Fischer-Tropsch synthesis.57. The method according to claim 56 wherein the catalyst comprises at least one of cobalt, ruthenium, or iron.58. The method according to claim 56 wherein the catalyst comprises a support selected from the group consisting of alumina, silica, titania, zirconia, and combinations thereof.59. The method according to claim 44 wherein the pressure differential between the slurry chamber and the filtrate chamber is less than 30 psi.60. The method according to claim 44 wherein the slurry linear velocity is regulated by the volumetric flow rate of the slurry through the filtration housing such that the slurry linear velocity increases as the thickness of the filter cake increases and the slurry linear velocity decreases as the thickness of the filter cake decreases.61. The method of claim 44 wherein the slurry is circulated to and from the filtration system in a circulation loop and the slurry linear velocity is regulated by controlling the configuration of the circulation loop.62. The method of claim 44 wherein the slurry linear velocity is regulated by the design of the filter housing.63. The method of claim 44 wherein the slurry is circulated between a Fischer-Tropsch reactor and the filtration system in a circulation loop and the slurry linear velocity is regulated by varying the gas hold up in the Fischer-Tropsch reactor.64. The method of claim 44 wherein the slurry linear velocity is regulated using valves to control the flow of slurry.65. The method according to claim 44 wherein the slurry linear velocity is regulated by adding a liquid stream to the slurry passing through the slurry chamber.

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Solid/liquid separation system for multiphase converters

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