JP2012082439A5

JP2012082439A5 -

Info

Publication number: JP2012082439A5
Application number: JP2011289168A
Authority: JP
Filing date: 2011-12-28
Publication date: 2012-07-19
Anticipated expiration: 2020-09-08

Claims

A method for conducting an olefin polymerization reaction comprising:
Recycling the olefin polymerization reaction mixture in the reaction zone of the olefin polymerization reactor;
Introducing the olefin-containing feedstock into the recycled olefin polymerization reaction mixture, wherein the olefin polymerization reaction mixture is recycled at a flow rate independent of the rate at which the feedstock is introduced into the reaction zone;
Introducing a catalyst composition comprising a catalyst and a catalyst modifier into the reaction mixture;
Bringing the polymerization reaction mixture to exothermic olefin polymerization conditions in the reaction zone in the presence of the catalyst composition;
Introducing a catalyst modifier into the recycled olefin polymerization reaction mixture at a rate independent of the rate at which the catalyst composition is introduced into the reaction zone.

A liquid phase polymerization method for producing polyisobutylene, comprising:
Providing a raw material containing isobutylene;
A step of supplying a catalyst composition comprising a complex of BF ₃ and the BF ₃ for the complexing agent,
Introducing the raw material and the catalyst composition into a reaction mixture within a reaction zone;
Intimately mixing the reaction mixture, the feedstock and the catalyst composition to produce a homogeneously mixed reaction mixture within the reaction zone;
Maintaining the homogeneously mixed reaction mixture in a homogeneously mixed state while polymerizing the isobutylene to form polyisobutylene;
Introducing an additional amount of the complexing agent into the homogeneously mixed reaction material at a rate independent of the rate of introduction of the catalyst composition;
Withdrawing a product stream comprising polyisobutylene from the reaction zone.

The reaction zone comprises a loop reactor, wherein the reaction mixture is continuously recirculated at a first volumetric flow rate, and the feedstock and the catalyst composition are continuously introduced at a second volumetric flow rate; The method of claim 2.

The method of claim 3, wherein the complexing agent comprises methanol.

The method of claim 2, wherein the homogeneously mixed reaction mixture is maintained at a temperature of at least 0 ° C. in the reaction zone.

The method of claim 2, comprising controlling the introduction of the raw material into the reaction zone and the extraction of the product stream from the reaction zone so that the residence time of isobutylene polymerized in the reaction zone is 4 minutes or less. Method.

6. Controlling introduction of the raw material into the reaction zone and withdrawal of the product stream from the reaction zone so that the residence time of isobutylene polymerized in the reaction zone is 4 minutes or less. Method.

Control of introduction of the raw material into the reaction zone and withdrawal of the product stream from the reaction zone such that the residence time of isobutylene polymerized in the reaction zone is 3 minutes or less. The method described.

4. The method of claim 3, wherein the ratio of the first volume flow rate to the second volume flow rate ranges from 20: 1 to 50: 1.

4. The method of claim 3, wherein the ratio of the first volume flow rate to the second volume flow rate ranges from 25: 1 to 40: 1.

4. The method of claim 3, wherein the ratio of the first volume flow rate to the second volume flow rate ranges from 28: 1 to 35: 1.

Supplying a raw material containing isobutylene;
A step of supplying a catalyst composition comprising a complex of BF ₃ and the BF ₃ for the complexing agent,
Introducing the raw material and the catalyst composition into a residual reaction mixture within a reaction zone;
Intimately mixing the residual reaction mixture, the feedstock and the catalyst composition to produce a homogeneously mixed reaction mixture within the reaction zone;
Maintaining the homogeneously mixed reaction mixture in a homogeneously mixed state, maintaining the mixture at a temperature of at least 0 ° C. while the reaction mixture is in the reaction zone, and polymerizing isobutylene in the mixture; Producing polyisobutylene;
Withdrawing a product stream comprising highly reactive polyisobutylene from the reaction zone, wherein the reaction zone is continuously recirculated of the reaction mixture at a first volumetric flow rate, and the feedstock and the catalyst composition A liquid phase polymerization process for producing highly reactive polyisobutylene comprising a loop reactor in which the product is continuously introduced at an overall second volumetric flow rate.

The method of claim 12, wherein the ratio of the first volume flow rate to the second volume flow rate ranges from 20: 1 to 50: 1.

13. The method of claim 12, wherein the ratio of the first volume flow rate to the second volume flow rate ranges from 25: 1 to 40: 1.

The method of claim 12, wherein the ratio of the first volume flow rate to the second volume flow rate ranges from 28: 1 to 35: 1.

A reactor for olefin polymerization,
  A catalyst defining a reaction zone and comprising an olefin polymerization reaction mixture inlet connection and an olefin polymerization reaction mixture outlet connection, the connection being in fluid communication with the reaction zone, wherein the catalyst comprises a catalyst and a catalyst modifier. A reactor arranged to promote an exothermic olefin polymerization reaction on the olefin polymerization reaction mixture in the presence of a composition;
  An inlet for introducing a raw material containing an olefin into the reaction mixture in the reaction zone;
  A recirculation system comprising a pump arranged to circulate the reaction mixture in the reaction zone at a flow rate independent of the rate at which the olefin-containing feedstock is introduced into the reaction zone;
  A catalyst composition inlet in fluid communication with the reaction zone for introducing the catalyst composition into the reaction mixture in the reaction zone; and
  At least one catalyst modification in fluid communication with the reaction zone for introducing a catalyst modifier into the reaction mixture in the reaction zone at a rate independent of the rate at which the catalyst composition is introduced into the reaction mixture in the reaction zone. Agent inlet
A reactor comprising:

The reactor for olefin polymerization according to claim 16, wherein the catalyst composition inlet is disposed away from the catalyst modifier inlet.

17. The reactor for olefin polymerization according to claim 16, wherein the catalyst composition inlet is connected to a pipe that is part of the recirculation system.