Shell and tube oxidation reactor with improved resistance to fouling

Patent metadata

Field	Value
Publication number	US-10286374-B2
Application number	US-201715825311-A
Country	US
Kind code	B2
Filing date	Nov 29, 2017
Priority date	Sep 24, 2012
Publication date	May 14, 2019
Grant date	May 14, 2019

Abstract

The present disclosure relates to a single shell open interstage reactor (“SSOI”). The SSOI comprises a first reaction stage, an interstage heat exchanger, an open interstage region, and a second reaction stage. The SSOI may be configured for upflow or downflow operation. Further, the open interstage region of the SSOI may comprise a supplemental oxidant feed. When the open interstage region comprises a supplemental oxidant feed, the SSOI may further comprise a supplemental oxidant mixing assembly. Processes for producing acrylic acid through the oxidation of propylene are also disclosed.

First claim

What is claimed is:

1. An upflow single shell open interstage reactor comprising:
a) a first shell-and-tube reaction stage comprising a plurality of reaction tubes, wherein the reaction tubes of the first reaction stage comprise a first catalyst;
b) an interstage heat exchanger;
c) an open interstage region; and
d) a second shell-and-tube reaction stage comprising a plurality of reaction tubes, wherein the reaction tubes of the second reaction stage comprise a second catalyst;
wherein said interstage heat exchanger is positioned between said first reaction stage and said open interstage region, and
wherein said reactor is configured for upflow operation.

2. The reactor of claim 1 , wherein said interstage heat exchanger is a shell-and-tube heat exchanger and comprises a plurality of interstage heat exchanger tubes.

3. The reactor of claim 2 , wherein said interstage heat exchanger tubes are coaxially continuous with the reaction tubes of the first reaction stage.

4. The reactor of claim 2 , wherein said interstage heat exchanger tubes comprise a catalyst retaining device.

5. The reactor of claim 4 , wherein said catalyst retaining device is capable of inducing turbulence within the said interstage heat exchanger tubes.

6. The reactor of claim 2 , wherein said interstage heat exchanger tubes comprise high void fraction, turbulence-inducing inserts.

7. The reactor of claim 6 , wherein said inserts have a void fraction of at least 85%.

8. The reactor of claim 1 , wherein said first reaction stage further comprises a first shellside coolant and said second reaction stage further comprises a second shellside coolant.

9. The reactor of claim 8 , wherein said first shellside coolant is controlled independently of said second shellside coolant.

10. The reactor of claim 2 , wherein said interstage heat exchanger further comprises a shellside heat exchanger coolant.

11. The reactor of claim 10 , wherein said first reaction stage further comprises a first shellside coolant that is controlled independently of said heat exchanger coolant.

12. The reactor of claim 1 , wherein said open interstage region is at least partially filled with at least one inert material.

13. The reactor of claim 12 , wherein said inert material has a surface area to bulk volume ratio of at least 78.7 m 2 /cubic m (24 ft 2 /cubic foot).

14. The reactor of claim 12 , wherein said inert material is present in an amount sufficient to provide at least 2790 m 2 (30,000 ft 2 ) of total surface area.

15. The reactor of claim 1 , wherein the reaction tubes of the first reaction stage have a different cross-sectional area than the reaction tubes of the second reaction stage.

16. The reactor of claim 15 , wherein the reaction tubes of the second reaction stage have a cross-sectional area at least 25% greater than the cross-sectional area of the reaction tubes of the first reaction stage.

17. The reactor of claim 16 , wherein the reaction tubes of the second reaction stage have a cross-sectional area at least 50% greater than the cross-sectional area of the reaction tubes of the first reaction stage.

18. The reactor of claim 1 , wherein the reaction tubes of the second reaction stage have an internal diameter greater than 22.3 mm (0.878 in).

19. The reactor of claim 18 , wherein the reaction tubes of the second reaction stage have an internal diameter greater than 25.4 mm (1 in).

20. The reactor of claim 1 , wherein said open interstage region comprises a supplemental oxidant supply line.

21. The reactor of claim 20 , wherein said open interstage region further comprises a supplemental oxidant mixing assembly.

22. The reactor of claim 21 , wherein said supplemental oxidant mixing assembly comprises a venturi mixer.

23. The reactor of claim 20 , wherein said supplemental oxidant supply line comprises an oxidant heat exchanger.

24. The reactor of claim 1 , further comprising inlet and outlet reactor heads, wherein at least one of said inlet reactor head and said outlet reactor head is removable.

25. The reactor of claim 1 , wherein at least one region chosen from the first reaction stage, the interstage heat exchanger, and the second reaction stage is configured for co-current coolant circulation.

26. The reactor of claim 1 , wherein at least one region chosen from the first reaction stage, the interstage heat exchanger, and the second reaction stage is configured for counter-current coolant circulation.

27. The reactor of claim 1 , wherein the second reaction stage comprises at least 22,000 reaction tubes.

28. The reactor of claim 27 , wherein the second reaction stage comprises at least 30,000 reaction tubes.

29. The reactor of claim 1 , wherein the number of reaction tubes in the first reaction stage is approximately equal to the number of reaction tubes in the second reaction stage.

30. The reactor of claim 1 , wherein the number of reaction tubes in the first reaction stage is different than the number of reaction tubes in the second reaction stage.

31. The reactor of claim 1 , wherein the reaction tubes in the second reaction stage are no greater than 4,500 mm (177 in) in length.

32. The reactor of claim 1 , wherein said interstage heat exchanger is capable of maintaining a process gas leaving the interstage heat exchanger at a temperature ranging from 240° C. to 280° C.

33. The reactor of claim 1 , wherein the reaction tubes of the first reaction stage have an internal diameter greater than 22.3 mm.

Assignees

• Arkema Inc

Inventors

• Decourcy Michael S
• Steinbach John L
• Dupont Nicolas
• Roundy Roger L

Classifications

• F28D21/0001

  Recuperative heat exchangers · CPC title

• B01J2208/025

  Two or more types of catalyst · CPC title

• C07C51/252

  of propene, butenes, acrolein or methacrolein · CPC title

• B01J2219/00594

  Gas-phase processes · CPC title

• C07C51/235

  of —CHO groups or primary alcohol groups · CPC title