Process for separating organic liquid solutes from their solvent mixtures

• US 4,349,415 A
• Filed: 09/28/1979
• Issued: 09/14/1982
• Est. Priority Date: 09/28/1979
• Status: Expired due to Term

• Current Assignee: CF Systems Corporation
• Original Assignee: Critical Care Systems Incorporated (Madison Dearborn Partners LLC)
• Inventors: Vivian, J. Edward, DeFilippi, Richard P.
• Primary Examiner(s): Bascomb, Jr., Wilbur L.
• Application Number:
  US06/079,935
• Time in Patent Office: 1,082 Days
• Field of Search: 203/14-19, 203/26, 203/49, 203/24, 203/73, 203/78, 203/80, 203/DIG. 20, 203/88, 203/98, 203/43-46, 203/39, 202/180, 210/634, 196/14, 196/52, 208/339, 208/352, 208/353, 208/361, 422/256-260, 560/261, 562/608, 568/410, 568/749, 568/869, 568/916
• US Class Current: 203/14
• CPC Class Codes: B01D 11/0407 the supercritical fluid acting as solvent for the solute
• CPC Class Codes: B01D 3/143 by two or more of a fractionation, separation or rectification step
• CPC Class Codes: B01D 3/322 Reboiler specifications
• CPC Class Codes: B01D 3/343 the substance being a gas
• CPC Class Codes: B01D 3/40 Extractive distillation

Abstract

Process and apparatus for extracting an organic liquid from an organic liquid solute/solvent mixture. The mixture is contacted with a fluid extractant which is at a temperature and pressure to render the extractant a solvent for the solute but not for the solvent. The resulting fluid extract of the solute is then depressurized to give a still feed which is distilled to form still overhead vapors and liquid still bottoms. The enthalpy required to effect this distillation is provided by compressing the still overhead vapors to heat them and indirectly to heat the still feed. The process is particularly suitable for separating mixtures which form azeotropes, e.g., oxygenated hydrocarbon/water mixtures. The energy required in this process is much less than that required to separate such mixtures by conventional distillation techniques.

Claims

1. A process for separating an organic liquid from an organic liquid/solvent mixture, comprising the steps of

(a) contacting a mixture of an organic liquid solute and a solvent for said solute with an extractant fluid under conditions of temperature and pressure to render said extractant fluid a solvent for said organic liquid solute but substantially less for said solvent, thereby forming a fluid extract of said organic liquid solute in said extractant fluid and a raffinate comprising said solvent with minor amounts of said extractant fluid and organic liquid solute, said extractant fluid being a gas at ordinary ambient conditions of temperature and pressure;

(b) separating said fluid extract and said raffinate;

(c) providing said fluid extract as a still feed separable into two phases by distillation;

(d) distilling said still feed to produce a still overhead vapor and liquid still bottoms;

(e) compressing said still overhead vapor to provide compressed vapor at an elevated temperature;

(f) effecting indirect heat exchange between said compressed vapor and said still bottoms to provide the thermal energy required in said distilling step, and to form a liquid condensate of said vapor;

3. A process in accordance with claim 1 wherein said extractant fluid is in the near critical liquid state.

4. A process in accordance with claim 1 wherein said extractant fluid is in the supercritical state.

5. A process in accordance with claim 1 wherein said extractant fluid is carbon dioxide, ethane or ethylene.

6. A process in accordance with claim 4 wherein said extractant fluid is carbon dioxide at a pressure between about 30 and about 150 atmospheres and between about 0°

C. and about 150°

C.

7. A process in accordance with claim 1 wherein said organic liquid solute is an oxygenated hydrocarbon, petroleum fraction, light hydrocarbon or aromatic hydrocarbon.

8. A process in accordance with claim 6 wherein said oxygenated hydrocarbon is an alcohol, ester, acid, aldehyde, ketone or polyhydric alcohol.

9. A process in accordance with claim 6 wherein said oxygenated hydrocarbon is methanol, ethanol, isopropanol normal propanol, phenol, vinyl acetate monomer, acetic acid, methyl ethyl ketone or glycerine.

10. A process in accordance with claim 1 wherein said solvent is a petroleum fraction or water.

11. A process in accordance with claim 1 wherein said mixture of organic liquid solute and solvent forms an azeotrope and said liquid bottoms product is richer in said solute than said azeotrope would be.

12. A process in accordance with claim 1 including the steps of generating mechanical energy in reducing said pressure in step (c) and using said mechanical energy in recompressing said still overhead vapor in step (e).

13. A process in accordance with claim 1 including the subjecting of said liquid bottoms product to a process comprising steps (a) through (h).

14. A process in accordance with claim 1 including the step of subjecting said liquid bottoms product to further distillation thereby to remove residual solvent.

15. A process in accordance with claim 1 wherein said flashing off of said extractant fluid from said raffinate comprises reducing the pressure of said raffinate to a level intermediate between that of said extracting step and atmospheric and separating said raffinate vapor flash from the liquid raffinate, said raffinate vapor flash being held at said intermediate pressure.

16. A process in accordance with claim 1 including the steps of withdrawing a portion of said recompressed vapor as a slip stream prior to effecting indirect heat exchange between said recompressed vapor and said still bottoms;

and effecting indirect heat exchange between said slip stream and said decompressed still bottoms prior to said separating said liquid organic product from said decompressed still bottoms.

17. A process in accordance with claim 15 including the step of adjusting the enthalpy of said slip stream prior to the effecting of indirect heat exchange between it and said decompressed still bottoms.

18. A process in accordance with claim 1 including the steps of recompressing said vapor flashes from steps (i) and (k) to render the resulting mixed fluid a solvent for said organic liquid solute;

combining said resulting fluid with said liquid condensate of said vapor from step (f); and

recycling the combined fluids as said extractant fluid in said contacting step.

19. A process in accordance with claim 17 including the step of adjusting the temperature of said mixed fluid prior to combining it with said liquid condensate.

20. A process in accordance with claim 17 including the step of adding makeup extractant fluid to said combined fluids prior to said recycling step.

21. A process in accordance with claim 17 including the steps of generating mechanical energy in reducing said pressure in step (c) and using said mechanical energy in recompressing said still overhead vapor in step (e).

22. A process in accordance with claim 17 including the steps of generating mechanical energy in reducing said pressure in step (c) and using said mechanical energy in recompressing said vapor flashes from steps (i) and (k).

24. A process in accordance with claim 22 wherein said oxygenated hydrocarbon is an alcohol, ester, acid, aldehyde, ketone or polyhydric alcohol.

25. A process in accordance with claim 22 wherein aqueous mixture forms an azeotrope and said liquid bottoms product is richer in said oxygenated hydrocarbon than said azeotrope would be.

26. A process in accordance with claim 22 including the steps of generating mechanical energy in reducing said pressure in step (c) and using said mechanical energy in recompressing said carbon dioxide vapor in step (e).

27. A process in accordance with claim 22 including the subjecting of said liquid bottoms product to a process comprising steps (a) through (h).

28. A process in accordance with claim 22 including the step of subjecting said liquid bottoms product to further distillation thereby to remove residual water.

29. A process in accordance with claim 22 wherein said solvent-condition carbon dioxide fluid is at about 65 atmospheres and 28°

C. in step (a);

said carbon dioxide vapor flashes are at about 10 atmospheres; and

said still feed of steps (c) is about 50 atmospheres and 15°

C.

30. A process in accordance with claim 22 including the steps of withdrawing a portion of said recompressed carbon dioxide from step (e) as a slip stream prior to step (f) and effecting indirect heat exchange between said slip stream and said decompressed still bottoms prior to said separating in step (k).

31. A process in accordance with claim 29 including the step of adjusting the enthalpy of said slip stream prior to the effecting of out-of-contact heat exchange between it and said decompressed still bottoms.

32. A process in accordance with claim 22 including the step of subjecting said liquid bottoms product to the process of steps (a)-(g) to provide a refined liquid bottoms product.

33. A process in accordance with claim 31 including the step of distilling said refined liquid bottoms product.

2. (g) recovering a liquid bottoms product comprising said liquid solute;

(h) recycling said liquid condensate as extractant fluid in said contacting step;

(i) flashing off said extractant fluid from said raffinate to provide a raffinate vapor flash;

(j) flashing off residual vapor from said still bottoms to form decompressed still bottoms; and

(k) separating liquid organic product from said decompressed still bottoms, thereby recovering said liquid bottoms product and producing a vapor flash.

23. A process for separating an oxygenated hydrocarbon liquid from an aqueous mixture, comprising the steps of

(a) contacting a mixture of an oxygenated hydrocarbon liquid and water with solvent-condition carbon dioxide fluid at a pressure between about 30 and about 150 atmospheres and a temperature between about 0°

and 150°

C., thereby forming a carbon dioxide fluid extract of said oxygenated hydrocarbon liquid and a raffinate comprising water with minor amounts of said carbon dioxide and oxygenated hydrocarbon liquid;

(b) separating said carbon dioxide fluid extract from said raffinate;

(c) reducing the pressure on said carbon dioxide fluid extract to form a still feed separable into two phases by distillation;

(d) distilling said still feed to produce a still overhead comprising essentially all carbon dioxide vapor and still bottoms;

(e) recompressing said carbon dioxide vapor from step (d) to provide recompressed carbon dioxide at a pressure essentially equivalent to that of said solvent-condition carbon dioxide used in step (a) and at a temperature above the boiling point of said still bottoms;

(f) effecting indirect heat exchange between said recompressed carbon dioxide and said still bottoms to provide the thermal energy required in said distilling step and to form a carbon dioxide liquid condensate;

(g) recovering a liquid bottoms product containing said oxygenated hydrocarbon;

(h) recycling said carbon dioxide liquid condensate as said solvent-condition carbon dioxide in step (a);

(i) flashing off said carbon dioxide from said raffinate to provide a raffinate carbon dioxide vapor flash;

(j) flashing off residual carbon dioxide from said still bottoms to form decompressed still bottoms;

(k) separating liquid oxygenated hydrocarbon product from said decompressed still bottoms and producing a carbon dioxide vapor flash;

(l) combining said carbon dioxide vapor flashes from steps (i) and (k);

(m) converting the combined vapor flashes to solvent-condition carbon dioxide fluid; and

(n) combining said carbon dioxide fluid of step (m) with said carbon dioxide fluid condensate of step (f).