Process for the epoxidation of propene

Patent metadata

Field	Value
Publication number	US-10399952-B2
Application number	US-201716086309-A
Country	US
Kind code	B2
Filing date	Mar 10, 2017
Priority date	Mar 21, 2016
Publication date	Sep 3, 2019
Grant date	Sep 3, 2019

Abstract

During start-up of a continuous epoxidation of propene with hydrogen peroxide in a methanol solvent with a shaped titanium silicalite catalyst in a tube bundle reactor with a cooling jacket, cooling medium is fed at the rate for full load of the reactor with a constant entry temperature of from 20° C. to 50° C., methanol solvent is fed at a rate of from 50 to 100% for full load of the reactor, hydrogen peroxide is fed at a rate that starts with no more than 10% of the rate for full load and is increased continuously or stepwise to maintain a maximum temperature in the fixed bed of no more than 60° C. and a difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20° C., and propene is fed at a rate of from 20 to 100% of the rate for full load, increasing the feeding rate when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load.

First claim

The invention claimed is:

1. A process for the epoxidation of propene by continuously reacting propene with hydrogen peroxide in a methanol solvent and in the presence of a shaped titanium silicalite catalyst; wherein:
a) the reaction is in a tube bundle reactor comprising a multitude of parallel reaction tubes and a cooling jacket enclosing the reaction tubes;
b) the catalyst is arranged as a fixed bed in the reaction tubes;
c) the molar ratio of propene to hydrogen peroxide is in the range of from 2.5:1 to 6:1 at full load of the reactor;
d) during start-up of the reaction with a fresh or a regenerated catalyst until full load of the reactor is reached:
i) cooling medium is fed to the cooling jacket at a constant rate for full load of the reactor, the entry temperature of the cooling medium being kept essentially constant at a value in the range of from 20° C. to 50° C.;
ii) methanol solvent is fed to the reaction tubes at a feeding rate of from 50 to 100% of a feeding rate for full load of the reactor;
iii) hydrogen peroxide is fed to the reaction tubes at a feeding rate that starts with no more than 10% of a feeding rate for full load of the reactor and is increased continuously or stepwise to the rate for full load of the reactor, increasing the feeding rate for hydrogen peroxide to maintain a maximum temperature in the fixed bed of no more than 60° C. and a temperature difference between the maximum temperature in the fixed bed and the cooling medium entry temperature of no more than 20° C.; and
iv) propene is fed to the reaction tubes at a feeding rate of from 20 to 100% of a feeding rate for full load of the reactor, increasing the feeding rate for propene when the molar ratio of propene to hydrogen peroxide reaches the molar ratio for full load of the reactor.

2. The process of claim 1 , wherein the parallel reaction tubes are arranged vertically and a mixture comprising propene, hydrogen peroxide and methanol solvent is passed through the reaction tubes in down-flow in trickle mode.

3. The process of claim 2 , wherein a first liquid feed stream comprising hydrogen peroxide and methanol solvent and a second liquid feed stream comprising propene are fed separately to the reaction tubes.

4. The process of claim 1 , wherein during start-up of the reaction the feeding rate for hydrogen peroxide is increased stepwise in steps of no more than 20% of the feeding rate for full load of the reactor.

5. The process of claim 4 , wherein the parallel reaction tubes are arranged vertically and a mixture comprising propene, hydrogen peroxide and methanol solvent is passed through the reaction tubes in down-flow in trickle mode.

6. The process of claim 5 , wherein a first liquid feed stream comprising hydrogen peroxide and methanol solvent and a second liquid feed stream comprising propene are fed separately to the reaction tubes.

7. The process of claim 4 , wherein during start-up of the reaction the feeding rate for hydrogen peroxide is increased stepwise in steps of no more than 10% of the feeding rate for full load of the reactor.

8. The process of claim 1 , wherein propene is used as a mixture with propane with a mass ratio of propane to the combined amounts of propane and propene of from 0.001 to 0.15.

9. The process of claim 8 , wherein the parallel reaction tubes are arranged vertically and a mixture comprising propene, hydrogen peroxide and methanol solvent is passed through the reaction tubes in down-flow in trickle mode.

10. The process of claim 9 , wherein a first liquid feed stream comprising hydrogen peroxide and methanol solvent and a second liquid feed stream comprising propene are fed separately to the reaction tubes.

11. The process of claim 8 , wherein during start-up of the reaction the feeding rate for hydrogen peroxide is increased stepwise in steps of no more than 20% of the feeding rate for full load of the reactor.

12. The process of claim 8 , wherein propene is used as a mixture with propane with a mass ratio of propane to the combined amounts of propane and propene of from 0.08 to 0.12.

13. The process of claim 12 , wherein during start-up of the reaction the feeding rate for hydrogen peroxide is increased stepwise in steps of no more than 10% of the feeding rate for full load of the reactor.

14. The process of claim 1 , wherein propene is reacted with hydrogen peroxide at a temperature of from 20 to 80° C. and a pressure of from 1.9 to 5.0 MPa.

15. The process of claim 14 , wherein the parallel reaction tubes are arranged vertically and a mixture comprising propene, hydrogen peroxide and methanol solvent is passed through the reaction tubes in down-flow in trickle mode.

16. The process of claim 15 , wherein a first liquid feed stream comprising hydrogen peroxide and methanol solvent and a second liquid feed stream comprising propene are fed separately to the reaction tubes.

17. The process of claim 14 , wherein during start-up of the reaction the feeding rate for hydrogen peroxide is increased stepwise in steps of no more than 20% of the feeding rate for full load of the reactor.

18. The process of claim 14 , wherein propene is used as a mixture with propane with a mass ratio of propane to the combined amounts of propane and propene of from 0.001 to 0.15.

19. The process of claim 14 , wherein during start-up of the reaction the feeding rate for hydrogen peroxide is increased stepwise in steps of no more than 10% of the feeding rate for full load of the reactor.

20. The process of claim 19 , wherein propene is used as a mixture with propane with a mass ratio of propane to the combined amounts of propane and propene of from 0.08 to 0.12.

Assignees

• Evonik Degussa Gmbh
• Thyssenkrupp Ind Solutions Ag

Inventors

• Wöll Wolfgang
• Brendel Marc
• Jaeger Bernd
• Bredemeyer Niels
• Kolbe Bärbel
• Ullrich Norbert
• Bernhard Maik

Classifications

• B01J8/067

  Heating or cooling the reactor (B01J8/062 takes precedence) · CPC title

• B01J8/0257

  in a cylindrical annular shaped bed · CPC title

• C07D301/36

  Use of additives, e.g. for stabilisation · CPC title

• C07D301/12 Primary

  with hydrogen peroxide or inorganic peroxides or peracids · CPC title

• B01J2208/00212

  Plates; Jackets; Cylinders · CPC title