Apparatus and method for controlling olefin polymerization process
View Patent ↗Apparatus for olefin polymerization includes one or more shell and tube olefin polymerization reactors, each of which has an olefin polymerization reaction mixture inlet connection and a crude polyolefin product outlet connection. Each reactor is equipped with a recirculation system including a pump arranged to circulate a reaction mixture through the tube side of the reactor independently of the introduction of olefin polymerization reaction mixture into the reactor. The apparatus may also include an inlet reaction mixture distribution manifold and an outlet polymerization reaction mixture collection manifold interconnecting the reactors for operation in parallel. The apparatus also includes catalyst composition and catalyst modifier inlets for each reactor arranged such that a catalyst modifier to may be introduced into each reactor at a rate which is independent of the introduction of catalyst composition.
1. A method for conducting an olefin polymerization reaction comprising:
recirculating an olefin polymerization reaction mixture in a reaction zone of an olefin polymerization reactor;
introducing an olefin containing feedstock into said recirculated olefin polymerization reaction mixture, said olefin polymerization reaction mixture being recirculated at a flow rate which is independent of the rate of introduction of said feedstock into said zone;
introducing a catalyst composition comprising a catalyst and a catalyst modifier into said reaction mixture;
subjecting said polymerization reaction mixture to exothermic olefin polymerization reaction conditions in said zone in the presence of said catalyst composition; and
introducing a catalyst modifier into said recirculating olefin polymerization reaction mixture at a rate which is independent of the rate of introduction of said catalyst composition into said zone.
2. A liquid phase polymerization process for preparing polyisobutylene, said process comprising:
providing a feedstock comprising isobutylene;
providing a catalyst composition comprising a complex of BF 3 and a complexing agent;
introducing said feedstock and said catalyst composition into a reaction mixture in a reaction zone;
intimately intermixing said reaction mixture, said feedstock and said catalyst composition to present an intimately intermixed reaction admixture in said reaction zone;
maintaining the intimately intermixed reaction admixture in its intimately intermixed condition while the same is in said reaction zone, to thereby cause the isobutylene therein to undergo polymerization to form polyisobutylene;
introducing an additional amount of said complexing agent into said intimately intermixed reaction admixture at a rate which is independent of the rate of introduction of said catalyst composition; and
withdrawing a product stream comprising polyisobutylene from said reaction zone.
3. A process as set forth in claim 2 , said reaction zone comprising a loop reactor wherein the reaction admixture is continuously recirculated at a first volumetric flow rate, and said feedstock and said catalyst composition are continuously introduced at a combined second volumetric flow rate.
4. A process as set forth in claim 3 , wherein said complexing agent comprises methanol.
5. A process as set forth in claim 4 , wherein the product is a highly reactive polyisobutylene and the ratio of BF 3 to methanol in said catalyst composition is no less than about 0.59:1.
6. A process as set forth in claim 4 , wherein the product is a highly reactive polyisobutylene and the ratio of BF 3 to methanol in said catalyst composition is in the range of from about 0.59:1 to about 0.62:1.
7. A process as set forth in claim 5 , wherein the product is a highly reactive polyisobutylene and a sufficient amount of methanol is independently introduced to cause the ratio of BF 3 to methanol in said intimately intermixed reaction admixture catalyst composition to be maintained in the range of from about 0.59:1 to about 0.60:1 during the course of the reaction.
8. A process as set forth in claim 6 , wherein a sufficient amount of methanol is independently introduced to cause the ratio of BF 3 to methanol in said intimately intermixed reaction admixture catalyst composition to be maintained at approximately 0.59:1 to about 0.62:1 during the course of the reaction.
9. A process as set forth in claim 3 , wherein said intimately intermixed reaction admixture catalyst composition is maintained at a temperature of at least about 0° C. while the same is in said reaction zone.
10. A process as set forth in claim 3 , including controlling the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 4 minutes.
11. A process as set forth in claim 9 , including controlling the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 4 minutes.
12. A process as set forth in claim 10 , wherein the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone are controlled such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 3 minutes.
13. A process as set forth in claim 11 , wherein the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone are controlled such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 3 minutes.
14. A process as set forth in claim 10 , wherein the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone are controlled such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 200 seconds.
15. A process as set forth in claim 11 , wherein the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone are controlled such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 200 seconds.
16. A process as set forth in claim 4 , wherein the product is a mid-range vinylidene content polyisobutylene and the ratio of BF 3 to methanol in said catalyst composition is about 1:1.
17. A process as set forth in claim 5 , wherein the product is a mid-range vinylidene content polyisobutylene and a sufficient amount of methanol is independently introduced to cause the ratio of BF 3 to methanol in said intimately intermixed reaction admixture catalyst composition to be maintained at approximately 1:1 during the course of the reaction.
18. A single-stage liquid phase polymerization process for preparing a polyolefin product having preselected properties, said process comprising:
providing a liquid feedstock comprising at least one olefinic component;
providing a catalyst composition comprising a complex of BF 3 and a complexing agent therefor, said complexing agent comprising a glycol or an aliphatic alcohol having a primary hydroxyl group and no hydrogen on a beta carbon, said complex being stable at temperatures needed to produce said polyolefin product;
introducing said feedstock and said catalyst composition into a residual reaction mixture in a loop reactor reaction zone;
recirculating the residual reaction mixture with the feedstock and the catalyst composition therein in said zone at a recirculation rate sufficient to cause intimate intermixing of the residual reaction mixture, the feedstock and the catalyst composition to thereby present a recirculating, intimately intermixed reaction admixture of the residual reaction mixture, the feedstock and the catalyst composition in said reaction zone;
maintaining the recirculating intimately intermixed reaction admixture in its intimately intermixed condition and removing heat of reaction from the reaction admixture at a rate calculated to provide a substantially constant reaction temperature in the reaction admixture while the same is recirculating in said reaction zone, said constant reaction temperature being at a level appropriate for causing olefinic components introduced in said feedstock to undergo polymerization to form said polyolefin product in the presence of said catalyst composition;
providing a catalyst modifier and introducing the same into said residual reaction mixture separately from said catalyst composition;
withdrawing a product stream comprising polyolefin product and catalyst composition from said reaction zone; and
controlling the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone such that the residence time of the olefinic components undergoing polymerization in the reaction zone is appropriate for production of said polyolefin product.
19. A liquid phase polymerization process for preparing low molecular weight, highly reactive polyisobutylene, said process comprising: providing a feedstock comprising isobutylene; providing a catalyst composition comprising a complex of BF 3 and a complexing agent therefor; introducing said feedstock and said catalyst composition into a residual reaction mixture in a reaction zone; intimately intermixing said residual reaction mixture, said feedstock and said catalyst composition to present an intimately intermixed reaction admixture in said reaction zone; maintaining the intimately intermixed reaction admixture in its intimately intermixed condition and keeping it at a temperature of at least about 0° C. while the same is in said reaction zone, to thereby cause the isobutylene therein to undergo polymerization to form said polyisobutylene; providing a catalyst modifier and introducing the same into said residual reaction mixture separately from said catalyst composition; withdrawing a product stream comprising low molecular weight, highly reactive polyisobutylene from said reaction zone; and controlling the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone such that the residence time of the isobutylene undergoing polymerization in the reaction zone is no greater than about 4 minutes.
20. A liquid phase polymerization process as set forth in claim 19 , wherein said polyisobutylene has an average molecular weight in the range of from about 500 to about 5000 and a vinylidene content of at least 70%, said catalyst composition comprises a complex of BF 3 and a C 1 to C 8 primary alcohol, and the amount of catalyst complex introduced into said reaction zone is controlled such that about 0.1 to about 10 millimoles of BF 3 are introduced for each mole of isobutylene introduced in said feedstock.
21. A liquid phase polymerization process as set forth in claim 19 , wherein said polyisobutylene has an average molecular weight in the range of from about 950 to about 1050, a polydispersity within the range of from about 1.3 to about 1.5 and a vinylidene content of at least about 80%, said feedstock comprises at least about 40% by weight isobutylene, said catalyst composition comprises a complex of BF 3 and methanol, the amount of catalyst complex introduced into said reaction zone is controlled such that about 0.5 to about 2 millimoles of BF 3 are introduced for each mole of isobutylene introduced in said feedstock, and the introduction of said feedstock into said reaction zone and the withdrawal of said product stream from the reaction zone are controlled such that the residence time of the isobutylene undergoing polymerization in the reaction zone is within the inclusive range of from about 45 to about 90 seconds.
22. A process as set forth in claim 19 , said reaction zone comprising a loop reactor wherein the reaction admixture is continuously recirculated at a first volumetric flow rate, and said feedstock and said catalyst composition are continuously introduced at a combined second volumetric flow rate.
23. A process as set forth in claim 20 , said reaction zone comprising a loop reactor wherein the reaction admixture is continuously recirculated at a first volumetric flow rate, and said feedstock and said catalyst composition are continuously introduced at a combined second volumetric flow rate.
24. A process as set forth in claim 21 , said reaction zone comprising a loop reactor wherein the reaction admixture is continuously recirculated at a first volumetric flow rate, and said feedstock and said catalyst composition are continuously introduced at a combined second volumetric flow rate.
25. A process as set forth in claim 18 or 19 , wherein said catalyst modifier comprises essentially the same composition as said complexing agent.
26. A process as set forth in claim 18 or 19 , wherein said catalyst modifier comprises a C 1 to C 8 primary alcohol.
27. A process as set forth in claim 18 or 19 , wherein said complexing agent comprises a C 1 to C 8 primary alcohol.
28. A process as set forth in claim 25 , wherein said same composition comprises a C 1 to C 8 primary alcohol.
29. A process as set forth in claim 18 or 19 , wherein said catalyst modifier comprises methanol.
30. A process as set forth in claim 18 or 19 , wherein said complexing agent comprises methanol.
31. A process as set forth in claim 25 , wherein said same composition comprises methanol.
32. A process as set forth in claim 19 , 22 , 23 or 24 , wherein said feedstock comprises at least about 30% by weight of said isobutylene.
33. A process as set forth in claim 18 , 19 , 20 or 21 , wherein the reaction zone is a tube side of a shell-and-tube reactor and the heat of reaction is removed simultaneously with its generation by circulation of a coolant in the shell side of the exchanger.
34. A process as set forth in claim 29 , wherein a heat transfer coefficient U of at least about 50 Btu/min ft 2 ° F. is maintained in the reaction zone.
35. A process as set forth in claim 18 , 19 , 20 or 21 , wherein said recirculation rate is sufficient to establish a Reynolds number of at least about 2000 in said zone.
36. A process as set forth in claim 18 , 19 , 20 or 21 , wherein is included a step of adding a quenching material capable of killing the catalyst to the withdrawn product stream.