Shell and tube oxidation reactor with improved resistance to fouling

Patent metadata

Field	Value
Publication number	US-9440903-B2
Application number	US-201213652522-A
Country	US
Kind code	B2
Filing date	Oct 16, 2012
Priority date	Sep 24, 2012
Publication date	Sep 13, 2016
Grant date	Sep 13, 2016

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. A process of making acrylic acid comprising the following steps in process flow order:
a) providing a mixed feed gas comprising propylene to a first reaction stage of a single shell open interstage shell and tube reactor comprising a plurality of reaction tubes, wherein the first reaction stage comprises a mixed metal oxide catalyst for oxidizing propylene to acrolein;
b) oxidizing the propylene in the first reaction stage to produce a process gas comprising acrolein;
c) cooling the process gas in an interstage heat exchanger disposed between the first reaction stage and a second reaction stage;
d) passing the cooled process gas through an open interstage region;
e) passing the process gas to a second shell and tube reaction stage comprising a plurality of reaction tubes, wherein the second reaction stage comprises a mixed metal oxide catalyst for oxidizing acrolein to acrylic acid; and
f) oxidizing the acrolein in the second reaction stage to produce a product gas comprising acrylic acid.

2. The process of claim 1 , wherein the mixed feed gas comprises at least 7.5 mol % propylene.

3. The process of claim 1 , wherein the mixed feed gas further comprises oxygen at an oxygen-to-propylene molar ratio of between 1.6 and 2.0.

4. The process of claim 1 , wherein the mixed feed gas further comprises water vapor at a water vapor-to-propylene molar ratio of about 1.2 or less.

5. The process of claim 1 , wherein the mixed feed gas is provided to the first reaction stage at a temperature greater than the dewpoint temperature of the mixed feed gas.

6. The process of claim 1 , wherein cooling the process gas comprises cooling the process gas to a temperature not greater than 280° C.

7. The process of claim 6 , wherein cooling the gas comprises cooling the process gas to a temperature ranging from 240° C. to 280° C.

8. The process of claim 1 , further comprising providing supplemental oxidant to the process gas in the open interstage region.

9. The process of claim 8 , further comprising mixing the process gas and supplemental oxidant in the open interstage region.

10. The process of claim 9 , wherein mixing the process gas and supplemental oxidant in the open interstage region comprises mixing in a mixing device.

11. The process of claim 1 , wherein the process gas is present in the interstage heat exchanger for a residence time of not more than 1.5 seconds.

12. The process of claim 1 , wherein the process gas is present in the interstage heat exchanger and the open interstage for a residence time of not more than 3 seconds.

13. The process of claim 1 , wherein passing the cooled process gas through an open interstage comprises removing foulants from the process gas by passing the process gas through an inert material having a total surface area of at least 930 m 2 .

14. The process of claim 13 , wherein the inert material has a total surface area of at least 2790 m 2 .

15. The process of claim 1 , wherein the mixed metal oxide catalyst in the first reaction stage comprises at least one compound selected from the group consisting of oxides of molybdenum, bismuth, and iron.

16. The process of claim 1 , wherein the mixed metal oxide catalyst in the second reaction stage comprises at least one compound selected from the group consisting of oxides of molybdenum and vanadium.

17. The process of claim 1 , further comprising circulating a coolant through the first reaction stage, the interstage heat exchanger, and the second reaction stage.

18. The process of claim 17 , wherein the coolant is circulated independently in at least one of the first reaction stage, the interstage heat exchanger, and the second reaction stage.

19. The process of claim 17 , wherein the coolant is circulated in a co-current configuration.

20. The process of claim 1 , wherein the interstage heat exchanger comprises inserts and cooling the process gas does not condense the process gas on the surface of the inserts.

21. The process of claim 1 , wherein the mass of catalyst in the second reaction stage is about 0.95 to about 1.65 times the mass of catalyst in the first reaction stage.

22. The process of claim 21 , wherein the mass of catalyst in the second reaction stage is about 1.25 to about 1.6 times the mass of catalyst in the first reaction stage.

23. The process of claim 1 , further comprising:
i) cooling the product gas to form a cooled product gas;
ii) transferring the cooled product gas to a solvent-free acrylic acid collection and purification system comprising a dehydration column and a finishing column;
iii) removing an overhead vapor stream comprising non-condensable gases and water vapor from the dehydration column;
iv) removing a side draw acrylic acid stream comprising at least 98 wt % acrylic acid from the finishing column; and
(v) removing a bottoms recirculation stream comprising heavy ends from the finishing column.

24. The process of claim 23 , further comprising processing the side draw acrylic acid stream in a melt crystallization process.

25. The process of claim 23 , further comprising transferring at least a portion of the bottoms recirculation stream comprising heavy ends to an ester process comprising a dimer cracker.

26. The process of claim 23 , further comprising:
vi) dividing the overhead vapor stream comprising non-condensable gases and water vapor into a recycle gas stream and a purge stream;
vii) returning the recycle gas stream to the single shell open interstage reactor; and
viii) processing the purge stream in one or more of a catalytic combustion unit, a thermal oxidizer, and a waste heat recovery system.

27. The process of claim 26 , wherein the mass flow rate of the recycle gas stream is between 5% and 50% of the mass flow rate of the overhead vapor stream comprising non-condensable gases and water vapor.

28. The process of claim 1 wherein the reaction tubes of the second reaction stage have a diameter greater than 22.3 mm.

Assignees

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

Inventors

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

Classifications

• F28D21/0001

  Recuperative heat exchangers · CPC title

• C07C51/252

  of propene, butenes, acrolein or methacrolein · CPC title

• B01J8/0453 Primary

  the beds being superimposed one above the other · CPC title

• B01J2219/30265

  Spiral · CPC title

• B01J2219/30226

  Cone or truncated cone · CPC title