Dicarboxylic acid production with enhanced energy recovery
The invention provides improved energy content in and shaft power recovery from off-gas from xylene oxidation reactions while at the same time minimizing wastewater treatment cost. More shaft power is produced using off-gas than is required to drive the main air compressor, even with preferred, relatively low oxidation temperatures. Simultaneously, an amount of wastewater greater than byproduct water from oxidation of xylene is kept in vapor form and treated along with off-gas pollutants in a self-sustaining (self-fueling) gas-phase thermal oxidative destruction unit. Optionally, off-gas is combined from multiple xylene oxidation reactors, comprising primary and/or secondary oxidation reactors and forming TPA and/or IPA. Optionally, air compressor condensate and caustic scrubber blowdown are used in a TPA process or as utility water, effectively eliminating normal flow of liquid wastewater effluent from a TPA plant. Optionally, PET off-gas containing the water of PET formation is treated in a shared thermal oxidative destruction unit, effectively eliminating normal flow of liquid wastewater effluent from a combined pX-to-TPA-to-PET plant.
1. A process for making terephthalic acid and/or isophthalic acid, said process comprising:
(a) oxidizing an aromatic compound in at least one oxidizer to thereby produce an oxidizer off-gas and an oxidizer slurry comprising terephthalic acid and/or isophthalic acid, wherein the at least one oxidizer comprises a bubble column reactor, and wherein the aromatic compound is at least one member selected from para-xylene and meta-xylene, wherein said oxidizer off-gas contains at least 12.4 kilograms of vapor per kilogram of said aromatic compound fed to said oxidizer; wherein said oxidizing is performed at a temperature of from 140 to 170° C. at a pressure of less than 8 bara;
(b) recovering hydrocarbyl compounds from said oxidizer off-gas in a solvent recovery system to thereby produce a hydrocarbyl-depleted off-gas comprising at least 3 kilograms of water vapor per kilogram of said aromatic compound fed to said oxidizer; and
(c) passing at least a portion of said hydrocarbyl-depleted off-gas through at least one turboexpander to thereby generate work, wherein said hydrocarbyl-depleted off-gas fed to said turboexpander comprises at least 3 kilograms of water vapor per kilogram of said aromatic compound fed to said oxidizer.
2. The process according to claim 1 wherein said oxidizer off-gas comprises at least 13.2 kilograms of vapor per kilogram of said aromatic compound fed to said oxidizer.
3. The process according to claim 1 wherein said oxidizer off-gas comprises vapor compounds including vaporized water and vaporized hydrocarbyl compounds.
4. The process according to claim 3 wherein said oxidizer off-gas comprises said vapor compounds in an amount of at least about 50 weight percent.
5. The process according to claim 1 wherein the mass of water vapor passed through said turboexpander is at least 50 percent of the amount of the mass of water exiting said solvent recovery system in said hydrocarbyl-depleted off-gas stream.
6. The process according to claim 5 wherein said hydrocarbyl-depleted off-gas is not subjected to thermal oxidative destruction (TOD) prior to entering said turboexpander.
7. The process according to claim 1 further comprising returning at least a portion of the recovered hydrocarbyl compounds to said oxidizer as recovered solvent.
8. The process according to claim 7 wherein at least 40 weight percent of said recovered solvent is supplied to said oxidizer at a temperature within 80° C. of the temperature of said oxidizer off-gas.
9. The process according to claim 1 further comprising subjecting a slurry comprising solid particles of said aromatic dicarboxylic acid and liquid solvent to solid-liquid separation and/or washing, further comprising recovering a filtrate solvent from said solid-liquid separation and/or washing step and returning at least a portion of said filtrate solvent to said oxidizer.
10. The process according to claim 9 wherein at least 40 weight percent of said filtrate solvent supplied to said oxidizer enters said oxidizer at a temperature of at least about 60° C.
11. The process according to claim 1 further comprising compressing air in an air compressor and feeding the resulting compressed air to said oxidizer.
12. The process according to claim 11 wherein said air compressor is at least partly powered by said turboexpander.
13. The process according to claim 12 wherein a turboexpander off-gas is discharged from said turboexpander, wherein the discharge pressure of said turboexpander off-gas is at least 0.05 barg and less than about 0.9 barg.
14. The process according to claim 1 wherein said hydrocarbyl-depleted off-gas fed to said at least one turboexpander comprises at least 3.3 kilograms of water vapor per kilogram of said aromatic compound fed to said oxidizer.
15. The process according to claim 1 wherein said hydrocarbyl-depleted off-gas fed to said at least one turboexpander comprises at least 40 mole percent water.
16. The process according to claim 15 further comprising removing at least about 10 weight percent of the water vapor present in said turboexpander off-gas as liquid water to thereby provided a condenser off-gas.
17. The process according to claim 16 wherein the discharge pressure of said turboexpander off-gas is at least −0.9 barg and less than about 0.3 barg.
18. The process according to claim 16 wherein said solvent recovery system does not employ an azeotropic distillation compound.
19. The process according to claim 1 wherein said aromatic compound is para-xylene.
20. A process for making terephthalic acid and/or isophthalic acid, said process comprising:
(a) oxidizing an aromatic compound in at least one oxidizer to thereby produce an oxidizer off-gas and an oxidizer slurry comprising an aromatic dicarboxylic acid, wherein the at least one oxidizer comprises a bubble column reactor, and wherein the aromatic compound is at least one member selected from para-xylene and meta-xylene, wherein said oxidizer off-gas contains at least 13.2 kilograms of vapor per kilogram of said aromatic compound fed to said oxidizer, wherein said oxidizer off-gas comprises at least about 50 weight percent of vapor compounds including vaporized water and vaporized hydrocarbyl compounds, wherein said oxidizing is performed at a temperature of from 140 to 170° C. at a pressure of less than 8 bara;
(b) recovering hydrocarbyl compounds from said oxidizer off-gas in a solvent recovery system to thereby produce a hydrocarbyl-depleted off-gas comprising at least 3.3 kilograms of water vapor per kilogram of said aromatic compound fed to said oxidizer; and
(c) passing at least a portion of said hydrocarbyl-depleted off-gas through at least one turboexpander to thereby generate work, wherein said hydrocarbyl-depleted off-gas fed to said turboexpander comprises at least 3.3 kilograms of water vapor per kilogram of said aromatic compound fed to said oxidizer, wherein the mass of water vapor passed through said turboexpander is at least 50 percent of the amount of the mass of water exiting said solvent recovery system in said hydrocarbyl-depleted off-gas stream.
21. The process according to claim 20 wherein said hydrocarbyl-depleted off-gas is not subjected to thermal oxidative destruction (TOD) prior to entering said turboexpander.
22. The process according to claim 20 further comprising returning at least a portion of the recovered hydrocarbyl compounds to said oxidizer as recovered solvent.
23. The process according to claim 22 wherein at least 40 weight percent of said recovered solvent is supplied to said oxidizer at a temperature within 80° C. of the temperature of said oxidizer off-gas.
24. The process according to claim 20 further comprising subjecting a slurry comprising solid particles of said aromatic dicarboxylic acid and liquid solvent to solid-liquid separation and/or washing, further comprising recovering a filtrate solvent from said solid-liquid separation and/or washing step and returning at least a portion of said filtrate solvent to said oxidizer.
25. The process according to claim 24 wherein at least 40 weight percent of said filtrate solvent supplied to said oxidizer enters said oxidizer at a temperature of at least about 60° C.
26. The process according to claim 20 further comprising compressing air in an air compressor and feeding the resulting compressed air to said oxidizer.
27. The process according to claim 26 wherein said air compressor is at least partly powered by said turboexpander.
28. The process according to claim 27 wherein a turboexpander off-gas is discharged from said turboexpander, wherein the discharge pressure of said turboexpander off-gas is at least 0.05 barg and less than about 0.9 barg.