Optimized liquid-phase oxidation
View Patent ↗Disclosed is an optimized process and apparatus for more efficiently and economically carrying out the liquid-phase oxidation of an oxidizable compound. Such liquid-phase oxidation is carried out in a bubble column reactor that provides for a highly efficient reaction at relatively low temperatures. When the oxidized compound is para-xylene and the product from the oxidation reaction is crude terephthalic acid (CTA), such CTA product can be purified and separated by more economical techniques than could be employed if the CTA were formed by a conventional high-temperature oxidation process.
1. An oxidation process for producing terephthalic acid, said process comprising:
(a) introducing a feed stream comprising para-xylene into a reaction zone of a bubble column reactor, wherein at least a portion of said reaction zone is defined by one or more upright sidewalls of said reactor, wherein at least 25 weight percent of said para-xylene enters said reaction zone at one or more locations spaced inwardly at least 0.05 D from said upright sidewalls, wherein said reaction zone has a maximum diameter (D); and
(b) oxidizing at least a portion of said para-xylene in a liquid phase of a three-phase reaction medium contained in said reaction zone, wherein said oxidizing forms crude terephthalic acid in said reaction medium, wherein the amount of solids present in said reaction medium is maintained in the range of from about 5 to about 40 weight percent on a time-averaged and volume-averaged basis.
2. The process of claim 1 wherein said oxidizing is carried out in a manner such that when said reaction zone is theoretically partitioned into 2,000 discrete horizontal slices of equal volume, less than 40 of said horizontal slices have an average gas hold-up less than 0.3, wherein the gas hold-up of said reaction medium is maintained above 0.4 on a time-averaged and volume-averaged basis.
3. The process of claim 1 wherein the amount of solids present in said reaction medium is maintained in the range of from about 10 to about 35 weight percent on a time-averaged and volume-averaged basis, wherein the gas hold-up of said reaction medium is maintained in the range of from about 0.6 to about 0.9 on a time-averaged and volume-averaged basis.
4. The process of claim 1 wherein the amount of solids present in said reaction medium is maintained in the range of from about 15 to about 30 weight percent on a time-averaged and volume-averaged basis, wherein the gas hold-up said reaction medium is maintained in the range of from 0.65 to 0.85 on a time-averaged and volume-averaged basis, wherein said oxidizing is carried out in a manner such that when said reaction zone is theoretically partitioned into 2,000 discrete horizontal slices of equal volume, less than 20 of said horizontal slices have a gas hold-up less than 0.3 on a time-averaged and volume-averaged basis.
5. The process of claim 1 wherein said oxidizing causes at least 10 weight percent of said para-xylene to form solid crude terephthalic acid particles in said reaction medium.
6. The process of claim 1 wherein said oxidizing is carried out in the presence of a catalyst system comprising cobalt.
7. The process of claim 6 wherein said catalyst system further comprises bromine and manganese.
8. The process of claim 1 wherein said reaction medium has a maximum height (H), a maximum width (W), and an H:W ratio of at least 3:1.
9. The process of claim 8 wherein said H:W ratio is in the range of from about 8:1 to about 20:1.
10. The process of claim 8 wherein said process further comprises introducing a predominately gas-phase oxidant stream comprising molecular oxygen into said reaction zone.
11. The process of claim 10 wherein a majority of said molecular oxygen enters said reaction zone within about 0.25 W of the bottom of said reaction zone.
12. The process of claim 10 wherein said predominately liquid-phase feed stream comprises acetic acid.
13. The process of claim 12 wherein at least 50 weight percent of said para-xylene enters said reaction zone within about 2.5 W of the lowest location where said molecular oxygen enters said reaction zone.
14. The process of claim 12 wherein said feed stream is introduced into said reaction zone via a plurality of feed openings, wherein at least two of said feed openings are vertically spaced from one another by at least 0.5 W.
15. The process of claim 1 wherein said para-xylene is introduced into said reaction zone at a mass flow rate of at least 8,000 kilograms per hour.
16. The process of claim 1 wherein said para-xylene is introduced into said reaction zone at a space-time rate in the range of from about 25 to about 400 kilograms per cubic meter per hour.
17. The process of claim 1 wherein said para-xylene is introduced into said bubble column reactor at a mass flow rate in the range of from about 18,000 to about 50,000 kilograms per hour, wherein said para-xylene is introduced into said reaction zone at a space-time rate in the range of from about 35 to about 150 kilograms per cubic meter per hour.
18. A process for producing terephthalic acid, said process comprising:
(a) introducing a feed stream comprising para-xylene into a reaction zone of a bubble column reactor, wherein at least a portion of said reaction zone is defined by one or more upright sidewalls of said reactor, wherein at least 25 weight percent of said para-xylene enters said reaction zone at one or more locations spaced inwardly at least 0.05 D from said upright sidewalls, wherein said reaction zone has a maximum diameter (D);
(b) oxidizing at least a portion of para-xylene in a liquid phase of a three-phase reaction medium contained in said reaction zone to thereby form solid crude terephthalic acid particles in said reaction medium, wherein the amount of solids present in said reaction medium is maintained in the range of from about 5 to about 40 weight percent on a time-averaged and volume-averaged basis; and
(c) oxidizing at least a portion of said solid crude terephthalic acid particles in a secondary oxidation reactor to thereby form purer terephthalic acid.
19. The process of claim 18 wherein said oxidizing is carried out in a manner such that when said reaction zone is theoretically partitioned into 2,000 discrete horizontal slices of equal volume, less than 40 of said horizontal slices have an average gas hold-up less than 0.3, wherein said reaction medium has a gas hold-up of at least 0.4 on a time-averaged and volume-averaged basis.
20. The process of claim 18 wherein the amount of solids present in said reaction medium is maintained in the range of from about 10 to about 35 weight percent on a time-averaged and volume-averaged basis.
21. The process of claim 18 wherein the gas hold-up of said reaction medium is maintained in the range of from about 0.6 to about 0.9 on a time-averaged and volume-averaged basis.
22. The process of claim 18 wherein the amount of solids present in said reaction medium is maintained in the range of from about 15 to about 30 weight percent on a time-averaged and volume-averaged basis, wherein the gas hold-up of said reaction medium is maintained in the range of from 0.65 to 0.85 on a time-averaged and volume-averaged basis, wherein said oxidizing is carried out in a manner such that when said reaction zone is theoretically partitioned into 2,000 discrete horizontal slices of equal volume, less than 20 of said horizontal slices have a gas hold-up less than 0.3 on a time-averaged and volume-averaged basis.
23. The process of claim 18 wherein said oxidizing in said secondary oxidation reactor decreases the average concentration of 4-CBA present in said solid crude terephthalic acid particles by at least 200 ppmw to thereby form said purer terephthalic acid.
24. The process of claim 18 wherein said solid crude terephthalic acid particles have an average 4-CBA concentration of at least 400 ppmw and said purer terephthalic acid has an average 4-CBA concentration of less than 400 ppmw.
25. The process of claim 18 wherein said oxidizing in said secondary oxidation reactor decreases the average concentration of 4-CBA in said solid crude terephthalic acid particles by at least 400 ppmw to thereby form said purer terephthalic acid, wherein said solid crude terephthalic acid particles have an average 4-CBA concentration of at least 800 ppmw and said purer terephthalic acid has an average 4-CBA concentration of less than 250 ppmw.
26. The process of claim 18 wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature at least 10° C. greater than the average temperature of said oxidizing in said bubble column reactor.
27. The process of claim 18 wherein said oxidizing in said bubble column reactor is carried out at an average temperature in the range of from about 125 to about 200° C., wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature in the range of from about 160 to about 240° C.
28. The process of claim 18 wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature in the range of from about 20 to about 80° C. greater than the average temperature of said oxidizing in said bubble column reactor, wherein said oxidizing in said bubble column reactor is carried out at an average temperature in the range of from about 140 to about 180° C., wherein said oxidizing in said secondary oxidation reactor is carried out at an average temperature in the range of from about 180 to about 220° C.
29. The process of claim 18 wherein said solid crude terephthalic acid particles have an average BET surface area of at least 0.6 meters squared per gram.
30. The process of claim 29 wherein said solid crude terephthalic acid particles have an average particle size in the range of from about 20 to about 150 microns.
31. The process of claim 30 wherein a substantial portion of said solid crude terephthalic acid particles comprise a plurality of agglomerated sub-particles having an average particle size in the range of from about 0.5 to about 30 microns.
32. The process of claim 31 wherein said solid crude terephthalic acid particles have an average particle size in the range of from about 30 to about 120 microns, wherein said sub-particles have an average particle size in the range of from about 1 to about 15 microns.
33. The process of claim 18 wherein said process further comprises recovering an initial slurry comprising a mother liquor and said solid crude terephthalic acid particles from said bubble column reactor, wherein said process further comprises replacing at least 50 weight percent of said mother liquor in said initial slurry with a replacement solvent to thereby provide a solvent-exchanged slurry comprising said replacement solvent and said solid crude terephthalic acid particles, wherein said process further comprises introducing said solvent-exchanged slurry into said secondary oxidation reactor.