PROCESS TO CONTINUOUSLY PREPARE A CYCLIC CARBONATE

Abstract

Process to continuously prepare a cyclic carbonate product by reacting an epoxide compound with carbon dioxide in the presence of a supported dimeric aluminium salen complex which complex is activated by a halide compound comprising the following steps, (a) contacting carbon dioxide with the epoxide compound in a suspension of liquid cyclic carbonate and the supported dimeric aluminium salen complex which complex is activated by a halide compound, (b) separating part of the cyclic carbonate product from the supported dimeric aluminium salen complex, (c) separating the halide compound from the cyclic carbonate product to obtain purified cyclic carbonate product, (d) use all or part of the halide compound as obtained in step (c) to activate deactivated supported dimeric salen complex.

Claims

1. A process to continuously prepare a cyclic carbonate product by reacting an epoxide compound with carbon dioxide in the presence of a supported dimeric aluminium salen complex which complex is activated by a halide compound comprising the following steps, (a) contacting carbon dioxide with the epoxide compound in a suspension of liquid cyclic carbonate and the supported dimeric aluminium salen complex which complex is activated by a halide compound, wherein the epoxide compound reacts with the carbon dioxide to the cyclic carbonate product and part of the supported dimeric salen complex deactivates, (b) separating part of the cyclic carbonate product from the supported dimeric aluminium salen complex, to obtain a mixture comprising of the cyclic carbonate product, carbon dioxide, epoxide compound and halide compound, (c) separating the halide compound from the cyclic carbonate product to obtain purified cyclic carbonate product, and (d) use all or part of the halide compound as obtained in step (c) to activate deactivated supported dimeric salen complex.

2. The process according to claim 1, wherein the temperature in step (a) is between 20 and 150 C. and the pressure is between 0.1 and 0.5 MPa and wherein temperature is below the boiling temperature of the product at the chosen pressure.

3. The process according to claim 1, wherein step (a) is performed in a continuously operated stirred reactor wherein carbon dioxide and epoxide compound are continuously supplied to the reactor and wherein part of the cyclic carbonate product is continuously withdrawn as part of a liquid stream.

4. The process according to claim 1, wherein the epoxide compound has 2 to 8 carbon atoms.

5. The process according to claim 4, wherein the epoxide compound is ethylene oxide, propylene oxide, butylene oxide, pentene oxide, glycidol or styrene oxide.

6. The process according to claim 1, wherein the separation in step (b) makes use of the different mass density and/or size between the cyclic carbonate and the supported dimeric aluminium salen complex.

7. The process according to claim 6, wherein the separation of step (b) is performed by means of a filter.

8. The process according to claim 6, wherein the separation of step (b) is performed using centrifugal forces.

9. The process according to claim 1, wherein step (c) is performed by distillation and wherein in the distillation step a mixture comprising of carbon dioxide, halide compound, the epoxide compound and the cyclic carbonate product is separated into separate streams of carbon dioxide, halide compound, epoxide compound and the cyclic carbonate product.

10. The process according to claim 9, wherein the content of epoxide compound in the mixture as obtained in step (b) is reduced to obtain a mixture having a reduced epoxide content which obtained mixture is separated in the distillation step (c).

11. The process according to claim 10, wherein the reduction of the epoxide compound is achieved by contacting the epoxide compound with carbon dioxide in the presence of supported dimeric aluminium salen complex in a second reaction step.

12. The process according to claim 1, wherein the deactivated supported dimeric aluminium salen complex is activated by contacting with the halide compound while performing step (a).

13. The process according to claim 1, wherein the deactivated supported dimeric aluminium salen complex is activated in a separate step (e) by contacting the deactivated supported dimeric aluminium salen complex with the halide compound in the presence of the cyclic carbonate product.

14. The process according to claim 13, wherein the molar ratio of halide compound and the supported dimeric aluminium salen complex is greater than 5:1 in step (e).

15. The process according to claim 1, wherein step (a) and (e) is performed in two or more parallel operated reactors and when step (e) is performed in one or more reactors step (a) is performed in at least one of the remaining reactors.

16. The process according to claim 1, wherein the supported dimeric aluminium salen complex is represented by the following formula: ##STR00004## wherein S represents a solid support connected to the nitrogen atom via an alkylene group, wherein the supported dimeric aluminium salen complex is activated by a halide compound and wherein X1 is tertiary butyl and X2 is hydrogen and wherein Et is an alkyl group having 1 to 10 carbon atoms.

17. The process according to claim 16, wherein the support S is composed of particles having an average diameter of between 10 and 2000 m.

18. The process according to claim 17, wherein the support S is a particle chosen from the group consisting of silica, alumina, titania, siliceous MCM-41 or siliceous MCM-48.

19. The process according to claim 1, wherein the halide compound is benzyl halide.

20. The process according to claim 19, wherein the benzyl halide is benzyl bromide.

Description

[0034] The invention will be illustrated by FIGS. 1-2 which illustrate a process to prepare propylene carbonate from carbon dioxide and propylene oxide. FIG. 1 shows 1 a continuously operated stirred reactor 1 provided with stirring means 2. To reactor 1 carbon dioxide in stream 3 and propylene oxide in stream 4 are continuously supplied. The reactor 1 further contains a suspension of liquid cyclic carbonate and the supported dimeric aluminium salen complex which complex is activated by a halide compound. From the reactor 1 a suspension of liquid cyclic carbonate, the supported dimeric aluminium salen complex which complex is activated by benzyl bromide, carbon dioxide and propylene oxide is continuously withdrawn as stream 6 and fed to a cross-flow filtration unit 7. In unit 7 a stream 8 is obtained which is a suspension of liquid propylene carbonate and enriched in supported dimeric aluminium salen complex which complex is activated by benzyl bromide and poor in carbon dioxide, propylene oxide and benzyl bromide. The unit 7 further yields a stream 9 which is a mixture of the propylene carbonate product, carbon dioxide, propylene oxide and halide compound as separated from the reaction mixture of stream 6. This stream 9 is fed to a distillation column 10. In distillation column 10 a purified propylene carbonate product is obtained as bottom stream 11, benzyl bromide as stream 12, propylene oxide and water as stream 13 and carbon dioxide as stream 14. Streams 13 and 14 may be fed to reactor 1. A purge may be provided for both streams 13 and 14 to avoid a build-up of non-reacting compounds. The stream 12 of benzyl bromide may be fed to a storage to be used in a regeneration step (e) of reactor 1. A purge may be provided for stream 12 to avoid a build-up of non-reacting compounds.

[0035] FIG. 2 shows a process flow scheme wherein stream 12 is continuously used to regenerate the catalyst complex of reactor 1. FIG. 2 shows the same reactors and unit operations as in FIG. 1. In addition a stream 15 is shown which directs part of stream 8 to a regeneration vessel 16. Also stream 12 is fed to vessel 16. In this way the catalyst complex can be regenerated with the halide compound of stream 12. The reactivated catalyst is fed to reactor 1 in stream 17.

[0036] FIG. 3 shows a scheme like in FIG. 1 except in that the filtered reaction mixture of stream 9 is now fed to a stripper-reactor 18. To this stripper-reactor 18 a flow of carbon dioxide 19 counter-currently contacts the reaction mixture. Part of the propylene oxide present in stream 9 will be stripped out of the mixture and returned to reactor 1 via stream 20. At the lower end of stripper-reactor 18 a mixture poor in propylene oxide is obtained as stream 21 and provided to a distillation column 10. The remaining streams are as in FIG. 1.