Process for starting-up an ethylene oxide reactor

• US 4,874,879 A
• Filed: 07/25/1988
• Issued: 10/17/1989
• Est. Priority Date: 07/25/1988
• Status: Expired due to Term

• Current Assignee: Shell Oil Company (Shell Plc)
• Original Assignee: Shell Oil Company (Shell Plc)
• Inventors: Baker, David S., Schuren, John G., Christiansen, Margot H., Johnson, Beamon M., Lauritzen, Ann M.
• Primary Examiner(s): Shine, W. J.
• Application Number:
  US07/224,049
• Time in Patent Office: 449 Days
• Field of Search: 549/534, 549/536
• US Class Current: 549/536
• CPC Class Codes: B01J 23/688 with manganese, technetium or rhenium
• CPC Class Codes: C07D 301/10 with catalysts containing silver or gold

Abstract

This invention relates to a process for starting up a fixed bed ethylene oxide reactor containing a catalyst comprising silver, alkali metal promoter and rhenium co-promoters supported on an alumina carrier which process comprises heating the reactor to slightly below normal operating conditions, passing an ethylene containing gas over the catalyst at a flow rate of about 20% of design, adding a chlorohydrocarbon moderator to the gas passing over the catalyst and after approximately 1 cubic centimeters of moderator (basis liquid) per cubic foot of catalyst has been added, then adding oxygen to the gas passing over the catalyst to initiate the ethylene oxidation reaction and subsequently raising the reactor temperature and gas flow rates to operating conditions.

Claims

1. A process for starting up a fixed bed ethylene oxide reactor containing a catalyst comprising silver, alkali metal promoter and rhenium co-promoter supported on an alumina carrier, which process comprises:

(a) heating the reactor to a temperature between about 400°

F. and 475°

F.,

(b) passing an ethylene-containing gas over the catalyst in the reactor at a flow rate between about 5 to about 40 percent of the design flow rate,

(c) adding a chlorohydrocarbon moderator to the gas passing over the catalyst and after between about 0.1 to about 10 cubic centimeters of moderator (basis liquid) per cubic foot of catalyst has been added,

(d) adding oxygen to the gas passing over catalyst, and raising the reactor temperature and gas flow rates to operating conditions.

2. The process of claim 1 wherein in step b) the ethylene-containing gas is passed over the reactor at a flow rate between about 15 to about 25 percent of the design flow rate.

3. The process of claim 1 wherein in step b) the ethylene-containing gas also contains nitrogen and methane.

4. The process of claim 1 wherein the chlorohydrocarbon moderator is a C₁ to C₈ chlorohydrocarbon.

5. The process of claim 4 wherein the chlorohydrocarbon moderator is a C₁ to C₄ chlorohydrocarbon.

6. The process of claim 5 wherein the chlorohydrocarbon moderator is a C₁ or C₂ chlorohydrocarbon.

7. The process of claim 6 wherein the chlorohydrocarbon moderator is selected from the group consisting of methyl chloride, ethyl chloride, ethylene dichloride, vinyl chloride and mixtures thereof.

8. The process of claim 1 wherein in step (c) from about 0.5 to about 5 cubic centimeters of moderator per cubic feet of catalyst is added.

9. The process of claim 8 wherein in step (c) from about 0.75 to about 2 cubic centimeters of moderator per cubic feet of catalyst has been added.

10. The process of claim 1 wherein in step (c) the moderator is added over a period of time ranging from about 1 to about 10 hours.

11. The process of claim 10 wherein in step (c) the moderator is added over a period of time ranging from about 2 to about 6 hours.

12. The process of claim 1 wherein in step (d) the reactor temperature and gas flow rates are raised to operating conditions over a period of time after the start of the oxygen addition ranging from about 15 minutes to about 6 hours.

13. The process of any one of claims 1-12 wherein nitrogen gas is passed over the catalyst prior to passing ethylene-containing gas of step (b) over the catalyst.

14. The process of claim 13 wherein the nitrogen gas is passed over the catalyst at a flow rate of between about 5 to about 40 percent of design flow rate.

15. The process of claim 14 wherein the nitrogen gas is passed over the catalyst at a flow rate of between about 15 to about 25 percent of design flow rate.

16. The process of claim 14 wherein the nitrogen is passed over the catalyst for a period of time ranging from about 1/2 to about 7 days.

17. The process of claim 15 wherein the nitrogen is passed over the catalyst for a period of time ranging from about 1/2 to about 7 days.