Oxidation system with internal secondary reactor
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. A process for making a polycarboxylic acid composition, said process comprising:
(a) subjecting a first portion of a multi-phase reaction medium to oxidation in a first reaction zone defined within an external reaction vessel;
(b) subjecting a second portion of said multi-phase reaction medium to oxidation in a second reaction zone defined within an internal reaction vessel, wherein said internal reaction vessel is at least partly disposed in said external reaction vessel; and
(c) withdrawing at least a portion of a slurry phase of said reaction medium from said second reaction zone for subsequent downstream processing, wherein said slurry phase comprises solid and liquid phases.
2. The process of claim 1 further comprising introducing an aromatic compound into said first reaction zone, wherein at least 80 weight percent of said aromatic compound introduced into said first reaction zone is oxidized in said first reaction zone in a liquid phase of said first portion of said reaction medium.
3. The process of claim 2 wherein said aromatic compound is para-xylene.
4. The process of claim 2 wherein step (b) includes oxidizing para-toluic acid present in said second portion of said reaction medium.
5. The process of claim 1 further comprising introducing a portion of said reaction medium into said second reaction zone, wherein the time-averaged concentration of para-toluic acid in a liquid phase of said slurry phase withdrawn from said second reaction zone is less than 50 percent of the time-averaged concentration of para-toluic acid in a liquid phase of said reaction medium introduced into said second reaction zone.
6. The process of claim 5 wherein the time-averaged concentration of para-toluic acid in said liquid phase of said reaction medium introduced into said second reaction zone is at least 500 ppmw, wherein the time-averaged concentration of para-toluic acid in said liquid phase of said slurry phase withdrawn from said second reaction zone is less than 250 ppmw.
7. The process of claim 1 further comprising subjecting at least a portion of said slurry phase withdrawn from said second reaction zone to oxidative digestion.
8. The process of claim 1 wherein said first and second portions of said reaction medium are maintained at substantially the same pressure at corresponding elevations in said first and second reaction zones, wherein said first and second portions of said reaction medium are maintained at substantially the same reaction temperature in said first and second reaction zones.
9. The process of claim 8 wherein said reaction temperature is in the range of from about 125 to about 200° C.
10. The process of claim 1 wherein said internal reaction vessel is located entirely inside said external reaction vessel.
11. The process of claim 1 wherein said internal reaction vessel is a bubble column reactor.
12. The process of claim 11 wherein said external reaction vessel is a bubble column reactor.
13. The process of claim 1 wherein said reaction medium is first processed in said first reaction zone and then in said second reaction zone.
14. The process of claim 1 wherein the ratio of the volume of said first reaction zone to the volume of said second reaction zone is in the range of from about 1:1 to about 100:1.
15. The process of claim 1 wherein said slurry phase flows in a generally downward direction in said second reaction zone.
16. The process of claim 1 wherein substantially all of the withdrawn slurry phase is removed from the lower 90 percent of the volume of said second reaction zone.
17. The process of claim 1 further comprising, introducing a portion of said reaction medium into said second reaction zone, wherein less than 50 weight percent of said reaction medium introduced into said second reaction zone enters said second reaction zone within the lower 90 percent of the volume of said second reaction zone.
18. The process of claim 1 wherein the mass-averaged residence time of said liquid phase in said second reaction zone is at least 1 minute.
19. The process of claim 1 wherein the time-averaged superficial velocity of said liquid phase at any elevation in said second reaction zone of less than 0.2 meters per second.
20. The process of claim 1 wherein step (a) includes, introducing molecular oxygen into said first reaction zone, wherein step (b) includes introducing additional molecular oxygen into said second reaction zone, wherein said additional molecular oxygen is molecular oxygen that is added to said second reaction zone in addition to the molecular oxygen already present in said reaction medium when said reaction medium enters said second reaction zone.
21. The process of claim 20 wherein the molar ratio of molecular oxygen introduced into said first reaction zone to said additional molecular oxygen introduced into said second reaction zone is at least 2:1.
22. The process of claim 1 wherein the ratio of the time-averaged superficial gas velocity of said first portion of said reaction medium at any elevation to the time-averaged superficial gas velocity of said second portion of said reaction medium at the same elevation is at least 1.25:1.
23. The process of claim 1 wherein the time-averaged superficial gas velocity of said first and second portions of said reaction medium at any elevation is at least 0.2 meters per second.
24. The process of claim 1 wherein the time-averaged superficial velocity of said slurry phase at any elevation in said second reaction zone is less than 0.2 meters per second.
25. The process of claim 1 further comprising introducing a portion of said reaction medium into an uppermost inlet of said second reaction zone, wherein at least a portion of the withdrawn slurry phase is withdrawn from a lowermost outlet of said second reaction zone.
26. The process of claim 25 further comprising introducing additional molecular oxygen into said second reaction zone at a location vertically-spaced from said uppermost inlet and said lowermost outlet, wherein said additional molecular oxygen is molecular oxygen that is added to said second reaction zone in addition to the molecular oxygen already present in said reaction medium when said reaction medium enters said second reaction zone.
27. The process of claim 25 wherein the ratio of the time-averaged gas hold-up of said reaction medium introduced into said uppermost inlet to the time-averaged gas hold-up of said slurry phase withdrawn from said lowermost outlet is at least 2:1.
28. The process of claim 25 wherein the time-averaged gas hold-up of said reaction medium introduced into said uppermost inlet is in the range of from about 0.4 to about 0.9 and the time-averaged gas hold-up of said product slurry withdrawn from said lowermost outlet is less than 0.1.
29. The process of claim 1 wherein less than 50 weight percent of said liquid phase withdrawn from said second reaction zone via openings in the lower 90 percent of the volume of said second reaction zone is introduced into said first reaction zone within 60 minutes after exiting said second reaction zone.
30. The process of claim 1 wherein the internal and external reaction vessels are aligned vertically such that the volumetric centroid of said second reaction zone is horizontally displaced from the volumetric centroid of said second reaction zone by less than 0.4 times the maximum horizontal diameter of said external reaction vessel.