A process for the polymerisation of olefins is disclosed wherein at least part of a stream, preferably a catalytically active stream, withdrawn from a polymerisation reactor is passed through a fractionator so as to remove hydrogen and active fines.
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The invention claimed is: 1. Process for the polymerisation of olefins comprising withdrawing at least part of a stream from a polymerisation reactor and passing the withdrawn stream through a fractionator which comprises a column having at least 3 equilibrium stages, wherein the heat content of th
The invention claimed is: 1. Process for the polymerisation of olefins comprising withdrawing at least part of a stream from a polymerisation reactor and passing the withdrawn stream through a fractionator which comprises a column having at least 3 equilibrium stages, wherein the heat content of the stream entering the fractionator is sufficient to provide at least 60% of the heat necessary for fractionation. 2. Process according to claim 1, which is a continuous process, in which the stream is continuously withdrawn. 3. Process according to claim 1, wherein the stream leaving the polymerisation reactor contains at least 10 vol % solid polymer. 4. Process according to claim 3, wherein the solid polymer fed into the fractionator has a particle size such that at least 50% of the polymer has a particle size of at least 7 μm. 5. Process according to claim 3, wherein at least 50% of the solid polymer has a particle size less than 100 μm. 6. Process according to claim 1, wherein the concentration of polymer in the stream fed into the fractionator is at least 0.002 vol %. 7. Process according to claim 6, wherein the polymer is solid and at least 50% of the solid polymer has a particle size less than 2000 μm. 8. Process according to claim 1, wherein the heat content of the stream entering the fractionator is sufficient to provide all of the heat necessary for fractionation. 9. Process for the polymerisation of olefins comprising withdrawing at least part of a stream from a polymerisation reactor and passing the withdrawn stream through a fractionator which comprises a column having at least 3 equilibrium stages, wherein the stream withdrawn from the polymerisation reactor is fractionated at a pressure such that the principal diluent of the stream is substantially condensed without compression using only cooling medium at a temperature between 15 and 60° C. 10. Process according to claim 9, wherein there is no reduction in pressure to below fractionation pressure applied to the stream between the reactor and the fractionator. 11. Process according to claim 1, wherein the equilibrium stages in the fractionator comprise sieve trays and/or dual flow trays. 12. Process for the polymerisation of olefins comprising withdrawing at least part of a stream from a polymerisation reactor and passing the withdrawn stream through a fractionator which comprises a column having at least 3 equilibrium stages, wherein at least the first two equilibrium stages in the fractionator are located above the feed location of the stream and have a stripping liquid flow that is at least 10 wt % of the vapour flow rate. 13. Process according to claim 12, wherein every equilibrium stage in the fractionator has a stripping liquid flow that is at least 10 wt % of its vapour flow rate. 14. Process according to claim 1, wherein the residence time of any solids in the fractionator is maintained at no more than 90 seconds. 15. Process according to claim 1, which process is a process for the polymerisation of ethylene or propylene utilising more than one reactor in series, and the principal diluent is an inert diluent or monomer. 16. Process according to claim 15, wherein hydrogen and/or comonomer is employed in at least one of the polymerisation reactors, and fractionation removes at least some of the hydrogen and/or comonomer from at least one of the streams containing the principal diluent prior to its distribution to a downstream reactor. 17. Process according to claim 16, wherein both comonomer and hydrogen are at least partly removed from the principal diluent in the same fractionator. 18. Process according to claim 15 wherein the fractionator is fed from more than one reactor and/or the fractionator feeds purified principal diluent to more than one reactor. 19. Process according to claim 15, wherein the ethylene is polymerised to form a polymer comprising at least 30 wt % of a low molecular weight component having a density of at least 0.965 g/cm3 and an MI2 of from 5 to 1000 g/10 min, and at least 30 wt % of a high molecular weight component having a density of from 0.910 to 0.940 g/cm3 and an MI5 of from 0.01 to 2 g/10 min. 20. Process according to claim 19, wherein the low molecular weight component is made in a reactor upstream of a reactor making the high molecular weight component. 21. Process according to claim 1, wherein the stream withdrawn from the polymerisation reactor is catalytically active. 22. Process according to claim 3, wherein the stream leaving the polymerisation reactor contains greater than 30 vol % solid polymer. 23. Process according to claim 22, wherein the stream leaving the polymerisation reactor contains greater than 40 vol % solid polymer. 24. Process according to claim 4, wherein the solid polymer fed into the fractionator has a particle size such that at least 50% of the polymer has a particle size of at least 10 μm. 25. Process according to claim 5, wherein at least 50% of the solid polymer has a particle size less than 50 μm. 26. Process according to claim 6, wherein the concentration of polymer in the stream fed into the fractionator is at least 30 vo1 %. 27. Process according to claim 26, wherein the concentration of polymer in the stream fed into the fractionator is at least 40 vol %. 28. Process according to claim 7, wherein at least 50% of the solid polymer has a particle size less than 1000 μm. 29. Process according to claim 9, wherein the cooling medium is water. 30. Process according to claim 14, wherein the residence time of any solids in the fractionator is maintained at no more than 30 seconds. 31. Process according to claim 15, wherein the principal diluent is selected from the group consisting of propylene, isobutane and hexane. 32. Process for the polymerisation of olefins comprising withdrawing at least part of a stream from a polymerisation reactor and passing the withdrawn stream through a fractionator with comprises a column having at least 3 equilibrium stages, which process is for the polymerisation of ethylene or propylene utilising more than one reactor in series, and the principal diluent is an inert diluent or monomer, wherein the fractionator is fed from more than one reactor and/or the fractionator feeds purified principal diluent to more than one reactor.
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이 특허에 인용된 특허 (2)
Sherk Fred T. (Bartlesville OK) Hanson Donald O. (Bartlesville OK), Monomer and diluent recovery.
Kreischer Bruce E. ; Verser Donald W. ; Hein James E., Process and apparatus for recovering diluent, monomer, and comonomer from a polymerization reactor effluent.
Bhandarkar, Maruti; Benham, Elizabeth A; Gonzales, Rebecca A.; Kufeld, Scott E.; Mutchler, Joel A; Gill, Catherine M.; Nguyen, Thanh T.; Odi, Timothy O., Polyolefin production with different diluents in multiple polymerization reactors.
Bhandarkar, Maruti; Benham, Elizabeth Ann; Gonzales, Rebecca A.; Kufeld, Scott E.; Mutchler, Joel A; Gill, Catherine M.; Nguyen, Thanh T.; Odi, Timothy O., Polyolefin production with different diluents in multiple polymerization reactors.
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