Continuous extraction of oil-containing vegetable matter with pressurized normally gaseous solvent

• US 5,041,245 A
• Filed: 03/10/1989
• Issued: 08/20/1991
• Est. Priority Date: 03/10/1989
• Status: Expired due to Fees

• Current Assignee: Bioseparsations Incorporated A US Corporation
• Original Assignee: Bioseparations Incorporated
• Inventors: Benado, Adam L.
• Primary Examiner(s): Dees, Jose G.
• Assistant Examiner(s): Carr, Deborah D.
• Application Number:
  US07/321,637
• Time in Patent Office: 893 Days
• Field of Search: 260/412, 260/412.4, 260/412.8, 260/428
• US Class Current: 554/10
• CPC Class Codes: B01D 11/0226 with the general transport direction of the solids parallel to the rotation axis of the conveyor, e.g. worm
• CPC Class Codes: B01D 11/028 Flow sheets
• CPC Class Codes: C11B 1/102 in counter-current; utilisation of an equipment wherein the material is conveyed by a screw
• CPC Class Codes: C11B 1/104 using super critical gases or vapours

Abstract

The oil in comminuted oil-containing vegetable matter is extracted by passing the vegetable matter through a closed extraction zone in contact preferably in countercurrent flow relation with a liquid extraction medium, which is a normally gaseous hydrocarbon, preferably propane, under a pressure sufficient to liquify the same up to about 250 psi, a temperature from about room temperature up to about 40°-50° C. and in sufficient volume to extract substantially the oil from such matter, e.g., a solvent feed ratio of about 1-3:1 by weight, the vegetable matter being continuously introduced into the zone by the steps comprising: advancing said vegetable matter through an elongated tubular screw-feeding stage communicating at its discharge end with one end of said extraction zone, subjecting said vegetable matter while within said screw-feeding stage to compacting pressure to create a region of compacted matter, and introducing under pressure into the compacted region a discrete innocuous normally liquid sealing medium which if different from said oil is capable of being at least substantially separated from the extracted oil, in an amount up to about 10% by weight of such matter which is effective to form the matter when compacted into a generally plastic mass, the magnitude of said compacting pressure in the absence of said medium being insufficient either to express said oil directly from said matter or densify said matter to a solid density capable of containing the pressure in the extraction zone. The preferred sealing medium upstream of the extraction zone is a recycled fraction of the extracted oil, and preferably a similar compaction zone is created in a screw-feeding stage at the discharge end of the extraction zone. The solvent and extracted oil are separated and recovered, the solvent being recycled for further extraction. The solid residue is freed of solvent and is useful, e.g., as defatted bran or meal. Preferably, the solvent-oil mixture after removal from the zone is subjected to a phase separation by raising its temperature and pressure to recover a liquid solvent phase containing a small amount of oil which can be reused as a solvent and an oil-enriched phase that can be freed of solvent by controlled volatilization. The solid residue is preferably freed of solvent by reducing the pressure thereon in at least two stages with heating, the solvent vapors being removed separately and compressed for recycling and reuse.

Claims

1. In a continuous method for extracting oil from communited oil-containing vegetable matter in which said vegetable matter is passed through a closed extraction zone in contact with a liquid extraction solvent medium wherein said extraction solvent medium is a normally gaseous hydrocarbon under a pressure in said extraction zone sufficient to liquify the same and up to about 250 psi, the improvement of continuously introducing said vegetable matter into said extraction zone for extraction therein by the steps comprising:

advancing said vegetable matter through an elongated tubular screw-feeding zone communicating at its discharge end with one end of said extraction zone, subjecting said vegetable matter while within said screw-feeding zone to compacting pressure to create a region of compacted vegetable matter, and introducing under pressure into the compacted matter region for admixture with the compacted matter passing therethrough an innocuous normally liquid sealing medium, which if different from said oil is capable of being separated from the extracted oil, in an amount up to about 10% by weight of said compacted matter, and sufficient when mixed with the compacted matter to form the same into a generally plastic mass capable of sustaining the pressure in said extraction zone, the magnitude of said compacting pressure in the absence of said sealing medium being insufficient either to express said oil directly from said vegetable matter or to densify said matter to a solid dam of a density sufficient to contain the pressure in said extraction zone.

2. The method of claim 1 wherein the flow of said vegetable matter through said extraction zone is countercurrent to the flow of said extraction solvent medium.

3. The method of claim 1 wherein said vegetable matter is a cereal bran.

4. The method of claim 3 wherein said cereal bran is rice bran.

5. The method of claim 1 wherein said sealing medium is oil previously extracted from said vegetable matter.

6. The method of claim 5 wherein a miscella of extracted oil in said solvent is removed from said extraction zone and the extracted oil is separated from said solvent medium;

and a fraction of the thus-separated oil is recycled and introduced into said region of compacted matter as said sealing medium.

7. The method of claim 1 including the steps of removing the residual vegetable matter after said extraction from said extraction zone through an additional elongated tubular screw-feeding zone communicating with said extraction zone, subjecting the residual matter to compacting pressure to create in said additional screw-feeding zone another region of compacted matter similar to that created in said first-mentioned screw-feeding zone and introducing into said another compacted region an innocuous normally liquid sealing medium which if different from the extracted oil is capable of being separated therefrom, in an amount up to about 10% by weight of the compacted matter in such region and effective to form said compacted matter into a dough-like plastic mass.

8. The method of claim 1 wherein said extraction zone is maintained at a temperature substantially below the critical temperature of the liquified hydrocarbon constituting said extraction solvent medium.

9. The method of claim 8 wherein said extraction zone is maintained under a temperature of up to about 50°

C.

10. The method of claim 9 wherein said extraction zone is maintained at about ambient temperature.

11. The method of claim 8 including the steps of removing a miscella of extracted oil in said extraction solvent medium continuously from said extraction zone at the pressure and temperature maintained in said zone, subjecting said miscella to mechanical pressure to pressurize the same to near-critical pressure and heating the same to near-critical temperature for said solvent medium, said near-critical temperature and pressure being selected to cause thermal phase-splittings of said miscella whereby said miscella separates into a light liquid phase consisting substantially entirely of said solvent medium and a dense liquid phase of an oil-enriched miscella, separating said liquid liquid phase and passing the same in heat exchange relation with fresh miscella subsequently removed from said extraction zone to transfer heat from said light phase to said subsequently removed miscella to cool the former and heat the latter, expanding the cooled light phase to reduce the pressure thereof while maintaining its liquid phase condition, the pressure and temperature of said light phase after said cooling and expansion generally corresponding to that of said extraction solvent medium in said extraction zone, and recycling the thus-cooled and expanded light phase to said extraction zone to comprise said extraction solvent medium.

12. The method of claim 11 comprising applying supplemental heating to the subsequently recovered miscella after heat exchange with said light phase to elevate the temperature thereof to said near-critical level.

13. The method of claim 12 which further comprises the steps of subjecting the oil-enriched dense liquid phase to at least two stages of evaporation while expanding the same to descending levels of pressure reduced from that of the thermal phase splitting, the pressure of the last such evaporation stage being ambient, to separate at least two fractions of solvent medium vapors under corresponding levels of pressure, separately recovering said solvent medium vapor fractions, subjecting each such fraction under extra-ambient pressure to at least one stage of high pressure pressurization as needed to raise the pressure thereof approximately to the pressure of the extraction zone, subjecting the ambient pressure fraction to at least one stage of low pressure pressurization followed by at least one stage of high pressure pressurization to raise the pressure thereof from to approximately that of the extraction zone, cooling the thus-pressurized fractions to the temperature of the extraction zone and thereby liquifying the same, and recycling the thus-liquified solvent fractions for reuse as the solvent medium in subsequent extraction.

14. The method of claim 13 wherein each of said evaporation stages is isothermal.

15. The method of claim 13 wherein the ambient pressure vapor fraction is pressurized in said low pressure stage to a pressure substantially equal to the pressure of one of the fractions separated under extra-ambient pressure and is combined with said latter fraction for pressurization in said high pressure stage.

16. The method of claim 13 wherein each of the expanded vapor fractions is heated after its expansion and before its separation and the high pressure pressurized fraction is cooled by passing the same in heat-exchange relation with at least the vapor fraction expanded to ambient pressure in the last evaporation stage, whereby said latter fraction is heated.

17. The method of claim 16 wherein said high pressure pressurized fraction after passage in heat-exchange relation with said ambient pressure fraction, is passed in heat-exchange relation with the oil-enriched dense phase after the expansion thereof for the first evaporation stage, whereby the latter becomes heated and the former cooled.

18. The method of claim 13 wherein the high pressure pressurized fraction is passed in heat-exchange relation with the oil-enriched fraction after the initial expansion of the latter for the first evaporation stage, whereby the latter is heated and the former is cooled.

19. The method of claim 1 which further comprises removing the solids residue from said extraction zone wet with solvent medium and subjecting it to at least two desolventizing stages with expansion to descending levels of pressure reduced from that of the extraction zone, the last such desolventizing stage being at ambient pressure, to recover a corresponding number of separate fractions of solvent medium vapor at graduated lower pressures, subjecting each such extra-ambient pressure fraction to high pressure pressurization to raise its pressure as needed to that of the extraction zone, subjecting the ambient pressure fraction to low pressure pressurization and at least one stage of high pressure pressurization to elevate the pressure thereof to the extraction pressure, cooling the thus-pressurized fractions to the extraction temperature to liquify the same and recycling the resulting liquified solvent medium for reuse in subsequent extraction.

20. The method of claim 19 wherein the ambient pressure fraction is pressurized in said low pressure pressurization to substantially the same pressure as one extra-ambient pressure fraction before high pressure pressurization thereof and is combined with the latter for high pressure pressurization and cooling to liquid condition.

21. The method of claim 19 wherein the vapor fraction from the low pressure pressurization is passed through said residue in said first stage to heat the same and assist in removal of the liquid solvent medium present therein.

22. In a continuous method for extracting rice oil from rice bran in which said rice bran is passed through a closed extraction zone in contact with a liquid extraction solvent medium wherein said extraction medium is a normally gaseous hydrocarbon under a pressure in said zone sufficient to liquify the normally gaseous hydrocarbon, the improvement comprising continuously introducing said rice bran into said extraction zone for extraction thereby the steps of:

advancing said rice bran through an elongated tubular screw-feeding zone communicating at its discharge end with one end of said extraction zone, subjecting said rice bran while within said screw-feeding zone to compacting pressure to create a region of compacted rice bran, and introducing under pressure into the compacted bran region for admixture with the compacted bran passing therethrough an innocuous normally liquid sealing medium, which if different from rice oil is capable of being separated from the extracted rice oil, in an amount up to about 10% by weight of said compacted rice bran and sufficient when mixed with said compacted bran to form the same into a generally plastic mass capable of sustaining the pressure in said extraction zone, the magnitude of said compacting pressure in the absence of said medium being insufficient either to express said rice oil directly from said rice bran or to densify said rice bran to a solid dam of a density sufficient to contain the pressure in said extraction chamber.

23. The method of claim 22, wherein the movement of said rice bran through said extraction zone is counter-current to the movement of said extraction solvent medium.

24. The method of claim 22, which further comprises removing the rice residue from said extraction zone wet with solvent medium and subjecting the rice bran residue to at least two desolventizing stages with expansion to descending levels of pressure reduced below the pressure of the extraction zone, the last such desolventizing stage being at ambient pressure, to, recover a corresponding number of separate fraction of solvent medium vapor at graduated lower pressures, subjecting each such extraambient pressure fraction to high-pressure pressurization to raise its pressure as needed to that of the extraction zone, subjecting the ambient pressure fraction to low-pressure pressurization and at least one stage of high-pressure pressurization to elevate the pressure thereof to the extraction pressure, cooling the thus-pressurized fractions to the extraction temperature to liquify the same and recycling the resulting liquified solvent medium for reuse in subsequent extraction.

25. The method of claim 24, wherein the ambient pressure fraction is pressurized in said low-pressure pressurization to substantially the same pressure as one extra-ambient pressure fraction before high-pressure pressurization thereof, and is combined with the latter for high-pressurization and cooling to liquid condition.

26. The method of claim 24, wherein the vapor fraction from the low-pressure pressurization is passed through said residue in said first desolventizing stage to heat the same and assist in removal of the liquid solvent medium present therein.

27. The method of claim 22, wherein said normally gaseous hydrocarbon is propane.

28. The method of claim 27, wherein the movement of said rice bran through said extraction zone is counter-current to the movement of said extraction solvent medium.

29. The method of claim 28, which further comprises removing the rice bran residue from said extraction zone wet with solvent medium and subjecting the rice bran residue to at least tow desolventizing stages with expansion to descending levels of pressure reduced less than the pressure of the extraction zone, the last such desolventing stage being at ambient pressure, to recover a corresponding number of separate fraction of propane vapor at graduated lower pressures, subjecting each such extra-ambient pressure fraction to high-pressure pressurization to raise its pressure as needed to that of the extraction zone, subjecting the ambient pressure fraction to low-pressure pressurization and at least one stage of high-pressure pressurization to elevate the pressure thereof to the extraction pressure, cooling the thus-pressurized fractions to the extraction temperature to liquify the same and recycle the resulting liquified propane for reuse in subsequent extraction.

30. The method of claim 29, wherein the ambient pressure fraction is pressurized in said low-pressure pressurization to substantially the same pressure as one extra-ambient pressure fraction before high-pressure pressurization, and is combined with the latter for high-pressurization and cooling to liquid condition.

31. The method of claim 30, wherein the vapor fraction from the low-pressure pressurization is passed through said residue in said first stage to heat the same and assist in removal of the liquid solvent present therein.