Method for operating a gas phase polymerization reactor
원문보기
IPC분류정보
국가/구분
United States(US) Patent
등록
국제특허분류(IPC7판)
C08F-002/00
C08F-004/00
C08F-012/08
C08F-012/00
출원번호
UP-0854345
(2004-05-26)
등록번호
US-7531606
(2009-07-01)
발명자
/ 주소
Hendrickson, Gregory G.
출원인 / 주소
Chevron Phillips Chemical Company LP
대리인 / 주소
Conley Rose, P.C.
인용정보
피인용 횟수 :
31인용 특허 :
11
초록▼
Disclosed herein is a method of operating a polymerization reactor for a polymerization reaction comprising modifying a recycle gas composition to increase the heat capacity of the recycle gas wherein the recycle gas composition is modified by reducing or eliminating the nitrogen concentration in th
Disclosed herein is a method of operating a polymerization reactor for a polymerization reaction comprising modifying a recycle gas composition to increase the heat capacity of the recycle gas wherein the recycle gas composition is modified by reducing or eliminating the nitrogen concentration in the recycle gas. In an embodiment, the nitrogen concentration is reduced or eliminated by reducing or eliminating one or more nitrogen input sources to the polymerization reactor and replacing the nitrogen with an alternate inert fluid (a gas or liquid that is inert to the catalyst and reactants). The alternate inert fluid has a higher heat capacity and a higher molecular weight than nitrogen. In an embodiment, the nitrogen utilized to convey a catalyst into the polymerization reactor is replaced with an alternate inert fluid. In an embodiment, the alternate inert fluid is ethane, propane, isobutane, or combinations thereof.
대표청구항▼
I claim: 1. A method of operating a gas phase fluidized bed polymerization reactor to produce a polymer product comprising: increasing a production rate of the same polymer product by modifying a composition of a recycle gas stream to the polymerization reactor to increase a heat capacity of the re
I claim: 1. A method of operating a gas phase fluidized bed polymerization reactor to produce a polymer product comprising: increasing a production rate of the same polymer product by modifying a composition of a recycle gas stream to the polymerization reactor to increase a heat capacity of the recycle gas stream while holding a condensate content of one or more inlet streams to the polymerization reactor at a value of less than or equal to about 17.4 weight percent, wherein modifying the recycle gas composition comprises adding an alternate inert fluid to the recycle gas and wherein the alternate inert fluid is noncondensable under reactor conditions. 2. The method of claim 1, wherein modifying the recycle gas composition further comprises reducing or eliminating nitrogen concentration in the recycle gas stream. 3. The method of claim 2, wherein reducing or eliminating nitrogen comprises: reducing or eliminating one or more nitrogen input sources to the polymerization reactor; and replacing the reduced or eliminated nitrogen with the alternate inert fluid. 4. The method of claim 3, wherein the polymerization reactor comprises one or more catalysts and one or more reactants, and wherein the alternate inert fluid is inert to the catalysts and the reactants. 5. The method of claim 3 wherein the nitrogen input source comprises nitrogen used to convey one or more catalysts into the polymerization reactor. 6. The method of claim 3 wherein the nitrogen input source comprises nitrogen present in a make-up gas stream fed to the polymerization reactor. 7. The method of claim 3 wherein the nitrogen input source comprises nitrogen used to blanket stored catalyst for use in the polymerization reactor. 8. The method of claim 3 wherein the nitrogen input source comprises nitrogen used to flush instruments taps in the polymerization reactor. 9. The method of claim 3, wherein the alternate inert fluid has a higher heat capacity and a higher molecular weight than nitrogen. 10. The method of claim 3, wherein the alternate inert fluid is ethane, propane, isobutane, or combinations thereof. 11. The method of claim 9, wherein the higher heat capacity and higher molecular weight of the alternate inert fluid increase heat removal from the polymerization reactor. 12. The method of claim 11, wherein the increased heat removal allows increased production capacity of the polymerization reactor. 13. The method of claim 1, wherein the polymerization reactor is a continuous, gas phase, fluidized catalyst bed, polymerization reactor. 14. The method of claim 13, wherein the catalyst is a polymerization catalyst comprising a chromium-based catalyst, a Ziegler-Natta catalyst, a metallocene catalyst, a vanadium based catalyst, a nickel based catalyst, or a combination thereof. 15. The method of claim 1, wherein the polymerization reaction polymerizes olefins into polyolefins. 16. The method of claim 1, wherein the polymerization reaction polymerizes a monomer and one or more comonomers into polyolefins. 17. The method of claim 16, wherein the monomer, comonomer, or both comprise alphaolefins. 18. The method of claim 16, wherein the monomer is ethylene, propylene, or combinations thereof. 19. The method of claim 16, wherein the one or more comonomers comprise propylene, 1-butene, 1-hexene, 1-octene, 1-decene, or combinations thereof. 20. The method of claim 1, wherein modifying the composition of the recycle gas stream increases heat removal from the polymerization reactor. 21. The method of claim 20, wherein the heat removal is increased by greater than about 5%. 22. The method of claim 20, wherein the heat removal is increased by greater than about 15%. 23. The method of claim 20, wherein the heat removal is increased by greater than about 25%. 24. The method of claim 20, wherein the heat removal is increased by greater than about 45%. 25. The method of claim 1, wherein increasing the heat capacity of the recycle gas stream increases production capacity of the polymerization reactor. 26. The method of claim 25, wherein the production capacity of the polymerization reactor is increased by greater than about 5%. 27. The method of claim 25, wherein the production capacity of the polymerization reactor is increased by greater than about 15%. 28. The method of claim 25, wherein the production capacity of the polymerization reactor is increased by greater than about 25%. 29. The method of claim 25, wherein the production capacity of the polymerization reactor is increased by greater than about 45%. 30. The method of claim 1, further comprising: reducing or eliminating one or more nitrogen input sources to the polymerization reactor; and replacing the reduced or eliminated nitrogen with an alternate inert fluid, wherein the alternate inert fluid is propane. 31. The method of claim 30, wherein isopentane concentration is adjusted to maintain the condensate content as calculated by the equations: propane=-8.1886(isopentane)2-2.5998(isopentane)+0. 6882 Q/Qbase=-4.8879(isopentane)2-2.2436 (isopentane)+1.5259 wherein propane is a mole fraction between about 0.057 and 0.074 and isopentane is a mole fraction between about 0.022 and 0.14, and Q/Qbase is the relative production capacities, calculated by dividing the production capability of a polymerization process replacing at least a portion of the nitrogen in the recycle stream with propane (Q) by the production capability of a polymerization process without replacing at least a portion of the nitrogen in the recycle stream with propane (Qbase). 32. The method of claim 1, further comprising: reducing or eliminating one or more nitrogen input sources to the polymerization reactor; and replacing the reduced or eliminated nitrogen with an alternate inert fluid, wherein the alternate inert fluid is isobutane. 33. The method of claim 32, wherein isopentane concentration is adjusted to maintain the condensate content as calculated by the equations: isobutane=-1.3636(isopentane)2-1.9918(isopentane)+0. 3776 Q/Qbase=-0.8938(isopentane)2-1.3021 (isopentane)+1.2481 wherein isobutane is a mole fraction between about 0.048 and 0.275 and isopentane is a mole fraction between about 0.05 and 0.15, and Q/Qbase is the relative production capacities, calculated by dividing the production capability of a polymerization process replacing at least a portion of the nitrogen in the recycle stream with isobutane by the production capability of a polymerization process without replacing at least a portion of the nitrogen in the recycle stream with isobutane. 34. A method of operating a gas phase fluidized bed polymerization reactor to produce a polymer product comprising: increasing a production rate of the same polymer product by replacing all or a portion of nitrogen fed into the reactor with an alternate inert fluid having a higher molecular weight and higher heat capacity than nitrogen while holding a condensate content of one or more inlet streams to the reactor at a value of less than or equal to about 17.4 weight percent, wherein the alternate inert fluid is noncondensable under reactor conditions. 35. The method of claim 34 further comprising adjusting isopentane concentration in the polymerization reactor to maintain the condensate content in one or more inlet streams. 36. A method of controlling heat removal in a gas phase fluidized bed polymerization reactor to produce a polymer product comprising: operating the reactor at a first steady state polymer production rate to produce the polymer product; increasing production of the same polymer product to a second steady state rate by replacing all or a portion of nitrogen fed into the reactor with an alternate inert fluid having a higher molecular weight and higher heat capacity than nitrogen, wherein the alternate inert fluid is noncondensable under reactor conditions; and maintaining a condensate content in one or more inlet streams to the polymerization reactor at a value of less than or equal to 17.4 weight percent during the first and second steady state polymer production rates. 37. The method of claim 36, wherein the alternate inert fluid is selected based on the molecular weight and heat capacity of the alternate inert fluid relative to nitrogen. 38. The method of claim 37, wherein the alternate inert fluid has a higher molecular weight and a higher heat capacity than nitrogen. 39. The method of claim 36, wherein the alternate inert fluid is ethane, propane, isobutane, or a combination thereof. 40. The method of claim 36, wherein the replacing all or a portion of the nitrogen increases the heat removal from the polymerization reactor. 41. The method of claim 40, wherein the heat removal is increased by greater than about 5%. 42. The method of claim 40, wherein the heat removal is increased by greater than about 15%. 43. The method of claim 40, wherein the heat removal is increased by greater than about 25%. 44. The method of claim 40, wherein the heat removal is increased by greater than about 45%. 45. A method of increasing production in a gas phase fluidized bed polymerization reactor to produce a polymer product comprising: selecting an alternate inert fluid and replacing all or a portion of nitrogen fed into the polymerization reactor with the alternate inert fluid, wherein the alternate inert fluid is noncondensable under reactor conditions; and maintaining a condensate content of less than or equal to 17.4 weight percent in one or more reactor inlet streams to the polymerization reactor, wherein the production rate of the same polymer product after replacing all or a portion of the nitrogen is greater than before replacing all or a portion of the nitrogen. 46. A method of increasing heat removal from a gas phase fluidized bed polymerization reactor to produce a polymer product comprising increasing heat capacity and molecular weight of a fluid used to convey catalyst to the polymerization reactor while increasing the production rate of the same polymer product and maintaining a condensate content of less than or equal to 17.4 weight percent in one or more inlet streams to the polymerization reactor, wherein the fluid is noncondensable under reactor conditions. 47. A method of reducing the amount of nitrogen build-up in a gas phase fluidized bed polymerization reactor to produce a polymer product comprising reducing or eliminating the amount of nitrogen used to convey catalyst into the polymerization reactor while increasing the production rate of the same polymer product and maintaining a condensate content of less than or equal to 17.4 weight percent in one or more inlet streams to the polymerization reactor, wherein the fluid is noncondensable under reactor conditions.
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이 특허에 인용된 특허 (11)
Hofferber James A. (Bartlesville OK), Control of a polymerization reaction.
Brady ; III Robert C. (Morristown NJ) Karol Frederick J. (Belle Mead NJ) Lynn Timothy R. (Hackettstown NJ) Jorgensen Robert J. (Belle Mead NJ) Kao Sun-Chueh (Belle Mead NJ) Wasserman Eric P. (Hopewel, Gas phase polymerization reactions utilizing soluble unsupported catalysts.
Mark Gregory Goode ; Mark Williams Blood ; William George Sheard, High condensing mode polyolefin production under turbulent conditions in a fluidized bed.
Jenkins ; III John M. (So. Charleston WV) Jones Russell L. (Chapel Hill NC) Jones Thomas M. (So. Charleston WV) Beret Samil (Danville CA), Method for fluidized bed polymerization.
Miles David L. (Neshanic NJ) Karol Frederick J. (Belle Mead NJ) Goeke George L. (Belle Mead NJ), Polymerization catalyst, process for preparing, and use for ethylene polymerization.
Robert Darrell Olson ; Timothy Joseph Howley, Polyolefin production using condensing mode in fluidized beds, with liquid phase enrichment and bed injection.
Hlavinka, Mark L.; Tso, Chung Ching; Inn, Yongwoo; Gagan, Deloris R.; Muninger, Randy S., Dual catalyst system for producing LLDPE copolymers with a narrow molecular weight distribution and improved processability.
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