[특허]Polymerisation control process

INEOS SALES (UK) LIMITED

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특허 상세정보

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Polymerisation control process

특허상세정보
국가/구분	United States(US) Patent 등록
국제특허분류(IPC7판)	C08F-002/34 C08F-010/00 B01J-008/44
출원번호	US-0885375 (2011-11-16)
등록번호	US-9394381 (2016-07-19)
우선권정보	EP-10192990 (2010-11-29)
국제출원번호	PCT/EP2011/070280 (2011-11-16)
§371/§102 date	20130514 (20130514)
국제공개번호	WO2012/072417 (2012-06-07)
발명자 / 주소	Chamayou, Jean-Louis Marissal, Daniel
출원인 / 주소	INEOS SALES (UK) LIMITED
대리인 / 주소	Nixon & Vanderhye P.C.
인용정보	피인용 횟수 : 0 인용 특허 : 4

초록

Process for maintaining a continuous gas-phase (co-) polymerization of olefins in a large fluidized bed reactor in a homogeneous mode while operating at high space time yield and condensation rate in the presence of a polymerization catalyst.

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1. Process for the continuous gas-phase (co-) polymerisation of olefins in a vertical fluidised bed reactor having a first volume of at least 250 m3, wherein D and V are respectively the diameter and the volume of the first volume of the reactor, and H is the height of the first volume of the reactor, being the distance between a fluidization grid at the bottom of the fluidized bed and the top of the first volume of the reactor, wherein the diameter D is at least 4 meters and the ratio H/D is higher than 3.75, said process being operated with a condensation rate higher than 15 wt %, in the presence of a polymerisation catalyst and with a space time yield equal or higher than 120 kg/(m3×h), and wherein the operations are controlled in order to maintain the parameter DT below 2.5, wherein DT=(1-0.016*Z*X)*K*S⁢⁢T⁢⁢Y*H*Heat⁢⁢Polym3600*Vf*Rho⁢⁢PE*Cp⁢⁢PEwhere:Z is the condensation rate expressed in wt %,X is the weight ratio between the liquid introduced directly in the fluidised bed above the fluidisation grid and the total liquid introduced into the reactor,K is a dimensionless calibration factor equal to 1.46,STY is the Space Time Yield expressed in [kg/(m3×h)],H is the distance between the bottom of the fluidised bed and the top of the first volume of the reactor (expressed in meter),Heat Polym is the heat of polymerisation expressed in Kcal/kg PolymerVf is the fluidization velocity of the fluidising gas (expressed in m/s),Rho PE is the polymer powder density expressed in Kg/m3, andCp PE is the heat capacity of the solid polymer expressed in Kcal/kg·C. 2. Process according to claim 1 wherein DT is maintained below 2.4. 3. Process for the continuous gas-phase (co-) polymerisation of olefins in a vertical fluidised bed reactor having a first volume of at least 250 m3 and a fluidisation grid at the bottom of the fluidised bed, said process being operated with a condensation rate higher than 15 wt % in the presence of a polymerisation catalyst and with a space time yield equal or higher than 120 kg/(m3×h), wherein the operations are controlled by reintroducing all the liquid directly into the fluidised bed, and wherein at least 50% of the liquid which is reintroduced directly into the fluidized bed is introduced at a height which is equal to or above 1 m above the fluidization grid. 4. Process for the continuous gas-phase (co-) polymerisation of olefins in a vertical fluidised bed reactor having a first volume of at least 250 m3 and a fluidisation grid at the bottom of the fluidised bed, said process being operated with a condensation rate higher than 15 wt % in the presence of a polymerisation catalyst and with a space time yield equal or higher than 120 kg/(m3×h), wherein the operations are controlled in order to maintain the polyolefin fluidised bed under homogeneous conditions by reintroducing the liquid partly below the fluidised bed through the fluidisation grid and partly directly into the fluidised bed, wherein the weight ratio (X) between the liquid introduced directly in the fluidised bed above the fluidisation grid and the total liquid introduced into the reactor is greater than 25%, and wherein at least 50% of the liquid which is reintroduced directly into the fluidized bed is introduced at a height which is equal to or above 1 m above the fluidization grid. 5. Process according to claim 1 wherein X is greater than 25%. 6. Process according to claim 1 wherein X is lower than 95%. 7. Process according to claim 1 wherein at least 50% of the liquid which is reintroduced directly into the fluidised bed is introduced at a height which is equal to or above 0.7 m above the fluidisation grid. 8. Process according to claim 1 wherein at least 50% of the liquid which is reintroduced directly into the fluidised bed is introduced at a height which is comprised between ¼H and ¾H. 9. Process according to claim 1 wherein the liquid reintroduced directly into the fluidised bed is introduced at a height lower than 0.9H. 10. Process according to claim 1 wherein the real height of the fluidized bed (h) is equal or higher than 0.85×H. 11. Process according to claim 1 wherein the real height of the fluidised (h) bed is equal or lower than 1.15×H. 12. Process according to claim 1 wherein the first volume of the reactor is at least 270 m3. 13. Process according to claim 1 wherein the first volume of the reactor is a cylinder. 14. Process according to claim 1 wherein the fluidized bed occupies at least 80% of the first volume of the reactor. 15. Process according to claim 1 wherein the fluidized bed occupies less than 120% of the first volume of the reactor. 16. Process according to claim 1 wherein the diameter D of the first volume of the reactor is at least 4.3 meters. 17. Process according to claim 1 wherein the diameter D of the first volume of the reactor is lower than 6 meters. 18. Process according to claim 1 wherein the ratio H/D of the reactor first volume is higher than 3.90. 19. Process according to claim 1 wherein the ratio H/D of the reactor first volume is lower than 5. 20. Process according to claim 1 wherein the condensation rate is equal or more than 17.5 weight percent. 21. Process according to claim 1 wherein the condensation rate is less than 60 percent. 22. Process according to claim 1 wherein the space time yield (“STY”) is higher than 150 kg/(m3×h). 23. Process according to claim 1 wherein the production rate of the polymer is of at least 30 tons per hour. 24. Process according to claim 1 wherein the fluidisation gas velocity is comprised between 70 and 80 cm/sec. 25. Process according to claim 3 wherein at least 50% of the liquid which is reintroduced directly into the fluidised bed is introduced at a height which is comprised between ¼H and ¾H. 26. Process according to claim 3 wherein the real height of the fluidized bed (h) is equal or higher than 0.85×H. 27. Process according to claim 3 wherein the real height of the fluidised (h) bed is equal or lower than 1.15×H. 28. Process according to claim 3 wherein the first volume of the reactor is at least 270 m3. 29. Process according to claim 3 wherein the first volume of the reactor is a cylinder. 30. Process according to claim 3 wherein the condensation rate is equal or more than 17.5 weight percent. 31. Process according to claim 3 wherein the condensation rate is less than 60 percent. 32. Process according to claim 3 wherein the space time yield (“STY”) is higher than 150 kg/(m3×h). 33. Process according to claim 3 wherein the production rate of the polymer is of at least 30 tons per hour. 34. Process according to claim 4 wherein X is greater than 50%. 35. Process according to claim 4 wherein X is lower than 95%. 36. Process according to claim 4 wherein at least 50% of the liquid which is reintroduced directly into the fluidised bed is introduced at a height which is comprised between ¼H and ¾H. 37. Process according to claim 4 wherein the real height of the fluidized bed (h) is equal or higher than 0.85×H. 38. Process according to claim 4 wherein the real height of the fluidised (h) bed is equal or lower than 1.15×H. 39. Process according to claim 4 wherein the first volume of the reactor is at least 270 m3. 40. Process according to claim 4 wherein the first volume of the reactor is a cylinder. 41. Process according to claim 4 wherein the condensation rate is equal or more than 17.5 weight percent. 42. Process according to claim 4 wherein the condensation rate is less than 60 percent. 43. Process according to claim 4 wherein the space time yield (“STY”) is higher than 150 kg/(m3×h). 44. Process according to claim 4 wherein the production rate of the polymer is of at least 30 tons per hour. 45. Process according to claim 1 wherein at least 50% of the liquid which is reintroduced directly into the fluidized bed is introduced at a height which is equal to or higher than 1 m above the fluidization grid. 46. Process according to claim 1 wherein the diameter D of the first volume of the reactor is at least 4.5 meters.

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Polymerisation control process

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