US2614111A - Process of refining glyceride oil in a liquid paraffinic solvent with a concentrated alcoholic alkali metal hydroxide solution - Google Patents
Process of refining glyceride oil in a liquid paraffinic solvent with a concentrated alcoholic alkali metal hydroxide solution Download PDFInfo
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- US2614111A US2614111A US69104A US6910449A US2614111A US 2614111 A US2614111 A US 2614111A US 69104 A US69104 A US 69104A US 6910449 A US6910449 A US 6910449A US 2614111 A US2614111 A US 2614111A
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- 238000000034 method Methods 0.000 title claims description 36
- 239000002904 solvent Substances 0.000 title claims description 23
- 238000007670 refining Methods 0.000 title claims description 21
- 150000008044 alkali metal hydroxides Chemical class 0.000 title claims description 17
- 230000001476 alcoholic effect Effects 0.000 title claims description 16
- 239000007788 liquid Substances 0.000 title claims description 10
- 125000005456 glyceride group Chemical group 0.000 title description 16
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 claims description 30
- 239000003518 caustics Substances 0.000 claims description 24
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 8
- 235000021588 free fatty acids Nutrition 0.000 claims description 7
- 239000003921 oil Substances 0.000 description 74
- 235000019198 oils Nutrition 0.000 description 72
- 235000019441 ethanol Nutrition 0.000 description 24
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 description 15
- 239000004215 Carbon black (E152) Substances 0.000 description 13
- 229930195733 hydrocarbon Natural products 0.000 description 13
- 150000002430 hydrocarbons Chemical class 0.000 description 13
- HEMHJVSKTPXQMS-UHFFFAOYSA-M Sodium hydroxide Chemical compound [OH-].[Na+] HEMHJVSKTPXQMS-UHFFFAOYSA-M 0.000 description 9
- HNRMPXKDFBEGFZ-UHFFFAOYSA-N 2,2-dimethylbutane Chemical compound CCC(C)(C)C HNRMPXKDFBEGFZ-UHFFFAOYSA-N 0.000 description 7
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 6
- 239000000470 constituent Substances 0.000 description 6
- 238000000605 extraction Methods 0.000 description 6
- 239000003549 soybean oil Substances 0.000 description 6
- 235000012424 soybean oil Nutrition 0.000 description 6
- 239000000203 mixture Substances 0.000 description 5
- KWYUFKZDYYNOTN-UHFFFAOYSA-M Potassium hydroxide Chemical group [OH-].[K+] KWYUFKZDYYNOTN-UHFFFAOYSA-M 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 239000012071 phase Substances 0.000 description 3
- 235000015112 vegetable and seed oil Nutrition 0.000 description 3
- 239000008158 vegetable oil Substances 0.000 description 3
- OFBQJSOFQDEBGM-UHFFFAOYSA-N Pentane Chemical group CCCCC OFBQJSOFQDEBGM-UHFFFAOYSA-N 0.000 description 2
- QAOWNCQODCNURD-UHFFFAOYSA-N Sulfuric acid Chemical compound OS(O)(=O)=O QAOWNCQODCNURD-UHFFFAOYSA-N 0.000 description 2
- 239000003153 chemical reaction reagent Substances 0.000 description 2
- 238000004821 distillation Methods 0.000 description 2
- 238000001035 drying Methods 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000010438 heat treatment Methods 0.000 description 2
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical group CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 2
- 238000006386 neutralization reaction Methods 0.000 description 2
- 238000002360 preparation method Methods 0.000 description 2
- 238000003825 pressing Methods 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 235000010469 Glycine max Nutrition 0.000 description 1
- 235000019483 Peanut oil Nutrition 0.000 description 1
- 239000010775 animal oil Substances 0.000 description 1
- 238000010923 batch production Methods 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 238000009835 boiling Methods 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 238000010924 continuous production Methods 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 235000005687 corn oil Nutrition 0.000 description 1
- 239000002285 corn oil Substances 0.000 description 1
- 238000005260 corrosion Methods 0.000 description 1
- 230000007797 corrosion Effects 0.000 description 1
- 239000002385 cottonseed oil Substances 0.000 description 1
- 235000012343 cottonseed oil Nutrition 0.000 description 1
- 210000003298 dental enamel Anatomy 0.000 description 1
- 230000001419 dependent effect Effects 0.000 description 1
- 229940126534 drug product Drugs 0.000 description 1
- -1 enamels Substances 0.000 description 1
- 238000007701 flash-distillation Methods 0.000 description 1
- 235000013305 food Nutrition 0.000 description 1
- 230000009931 harmful effect Effects 0.000 description 1
- 230000007062 hydrolysis Effects 0.000 description 1
- 238000006460 hydrolysis reaction Methods 0.000 description 1
- 239000000944 linseed oil Substances 0.000 description 1
- 235000021388 linseed oil Nutrition 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 229910000000 metal hydroxide Inorganic materials 0.000 description 1
- 150000004692 metal hydroxides Chemical class 0.000 description 1
- 125000005244 neohexyl group Chemical group [H]C([H])([H])C(C([H])([H])[H])(C([H])([H])[H])C([H])([H])C([H])([H])* 0.000 description 1
- 230000003472 neutralizing effect Effects 0.000 description 1
- 239000003973 paint Substances 0.000 description 1
- 239000000312 peanut oil Substances 0.000 description 1
- 239000000825 pharmaceutical preparation Substances 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- 229920003023 plastic Polymers 0.000 description 1
- 239000000376 reactant Substances 0.000 description 1
- 239000000344 soap Substances 0.000 description 1
- 229910052708 sodium Inorganic materials 0.000 description 1
- 239000011734 sodium Substances 0.000 description 1
- 229920003002 synthetic resin Polymers 0.000 description 1
- 239000000057 synthetic resin Substances 0.000 description 1
- 239000002383 tung oil Substances 0.000 description 1
- 230000008016 vaporization Effects 0.000 description 1
- 239000002966 varnish Substances 0.000 description 1
Images
Classifications
-
- C—CHEMISTRY; METALLURGY
- C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
- C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
- C11B3/00—Refining fats or fatty oils
- C11B3/02—Refining fats or fatty oils by chemical reaction
- C11B3/06—Refining fats or fatty oils by chemical reaction with bases
Definitions
- glyceride oils can be refined by a single treatment with an alcoholic solution of an alkali metal hydroxide. To my knowledge, it has never been tried or even realized that'the extraction and neutralization steps could be combined into a single treatment, but I have found thatglyceride oils can be efiiciently refined by such asingle treatment.
- a solvent-oil miscella by dissolving one part of alcohol, ethyl or isopropyl alcohol may be used instead. It is not necessary that absolute alcohol be used but the alcoholic content should be between 75 and 100 per cent, the higher water contents being desirable when operating at higher temperatures, as hereafter disclosed. I may use from 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil treated, the exact amount extraction, I prefer that the contact time be between 5 and minutes and that the temperature be between 0 and 30 0., although tempera' tures between 20 to 130" C. may be employed. K
- the pressure is adjusted to maintain the reactants in the liquid phase.
- lThevolume ratio of alcohol to glyceride oil should be from 0.2 1 to :1, the preferred range beingfrom 2:1 to 20:1.
- the mixture is allowed to settle and the oily miscella is separated from the spent caustic solution.
- the oil and spent caustic solutions can be separated by gravity when operating under preferred conditions of high solvent to oil ratio because the miscella will be of suificiently low density, to allow the spent caustic to settle.
- the separation may be made by means of a centrifuge or its equivalent.
- the paraffinic solvent added to the oil in forming the. original miscella is removed by distillation, preferably, at atmospheric pressure, the temperature vto which it must be heated, of course, being dependent on the boiling point of the solvent used. It is not desirable to heat the oil to a much higher temperature than is necessary to distill the solvent.
- My invention may be'carried out as a batch process or the process may be continuous, as shown in the drawing.
- the drawing represents the apparatus adapted to carrying out a process wherein the density of miscella is suificiently below that of the caustic solution to permit countercurrent flow of liquids through the extractor.
- the separator which maybe a centrifuge or any equivalent, permits more complete separation of miscella and spent caustic.
- the concentration of caustic in the alcohol-caustic treating fluid is. lower than the concentration normally employed in the neutralizing fluid of a two-step process. This means less corrosion of equipment and less hydrolysis of the oil during treatment. Numerous other advantages will be apparent to those skilled in the art.
- mixtures of the suitable solvents and/or mixtures of the caustic materials is fully within the intended scope of my invention.
- My invention may be employed in the refining of innumerable oils which can be refined by caustic treatment and alcohol extraction.
- a glycerlde oil which comprises intimately contacting a solventoil miscella comprising a solution of said oil in from 1 to 6 volumes of a liquid hydrocarbon for a period of time from 5 to 30 minutes at a temperature of from 20 to C. with an alcoholic alkali metal hydroxide solution consisting essentially of from '75 to 100 per cent alcohol, 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil and water whenever the concentration of the alcohol employed is less than 100 per cent the ratio of alcohol to oil being from .2 to 50 volumes of said alcohol per volume of oil, separating the miscella from the caustic solution and separating the resulting miscella into the solvent and oil fractions.
- a glyceride oil which comprises intimately contacting a solventoil miscella comprising a solution of said oil in from 1 to 6 volumes of a liquid paraffinic hydrocarbon for from 5 to 10 minutes at a tempera ture from 0 to C. with an alcoholic caustic solution containing essentially from 75 to 100 per cent methyl alcohol, from 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil and water whenever the concentration of the alcohol employed is less than 100 per cent, the ratio of alcohol to oil being from 2 to 20 volumes of said alcohol per volume of oil, separating the miscella from the caustic solution and separating the resulting miscella into the solvent and oil fractions.
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- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Life Sciences & Earth Sciences (AREA)
- General Chemical & Material Sciences (AREA)
- Microbiology (AREA)
- Engineering & Computer Science (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- Wood Science & Technology (AREA)
- Organic Chemistry (AREA)
- Fats And Perfumes (AREA)
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
Description
Oct. 14, 1952 AYERS 2,614,111
PROCESS OF REFINING GLYCERIDE OIL IN A LIQUID PARAFFINIC SOLVENT WITH A CONCENTRATED ALCOHOLIC ALKALI METAL HYDROXIDE SOLUTION Filed Jan. 4, 1949 HOIDVHLXB NOLLV'HLLSIG HSV'IJ INVENTOR.
A.L. AYERS M5 v. {E N R O T T A Y Patented Oct. 14, 1952 PROCESS OF'REFINING GLYCERIDE OIL IN A LIQUID 'PARAFFINIC SOLVENT WITH A CONCENTRATED ALCOHOLIC ALKALI METAL HYDROXIDE SOLUTION Arnold L. Ayers, Bartlesville, 0kla., assignor t0 Phillips Petroleum Company, a corporation of Delaware Application January 4, 1949, Serial No. 69,104
14 Claims. 1
This invention relates to a method of treating glyceride oils. Ina .more specific aspect, it relates to a method of treating glyceride oils to remove undesirable constituents. In another specific aspect, it relates to a method for removing free fatty acids, color bodies, non-drying constituents, and break formers from a glyceri'de oil. .In still another specific aspect, it relates to a single-treatment methodof refining glyceride oils. More specifically, it relates to a method of refining soy bean oil. c
The glyceride oils with which this invention is concerned, are animal and vegetable oils, the latter of which are obtained from seeds, usually by pressing or by extraction with a suitable solvent. Some of the commonly used glyceride oils are linseed oil, tung oil, soy bean oil, cotton seed oil, corn oil, and peanut oil. While these oils have wide use in the preparation of foods, my invention is likewise concerned with the preparation of these oils as film-forming constituents, such as in paints, varnishes, enamels, synthetic resins, soap, plastics, drug products, and the like.
Ordinarily, glyceride oils, both those obtained by pressing and by extraction with solvents contain about 0.5 to 1 per cent of phosphatides and 1 to 2 per cent of free fatty acids. In addition, there is a certain content of color bodies, nondrying constituents, and materials which cause break or sludge formation upon heating. In preparing oils for such industrial uses,it isinecessary'that these undesirable constituents be removed.
Conventional methods of refining vegetable oils involve the use of large volumes of concentrated.
reagents such as sulfuric acid or sodium hydroxide, which often tend to char or coagulatethe by-products :of the oil. In addition, these reagents have a harmful effect .on .the. drying or film-forming characteristics of the oil. In my copending application, Serial No. 17,105, filed March25, 1948, for A Process for Refining Soy 'Be'an'Oil, I have disclosed a method of refining soy bean oil comprising the steps of extracting the oil with an alcohol-water solution followed by treatment with a dilute caustic solution.
I have now discovered a method of refining vegetable oils which involves a single treatment with an alcoholic solution of an alkali metal hydroxide.
It is therefore an object of my invention to provide a method .for refining glycerid'e oils wherein a minimum amount of equipment is required.
It is another object of my invention to provide a 2 a method for removing :undesirable constituents from a glyceride oil.
It is still another .object of .my invention to provide .a single-treatment method for refining glyceride oils.
It is another object of my invention to'provide a method for refining soy bean oil with aminimum loss of oil.
Other objects and advantages of my'invention will be apparent'to those skilled in the art upon reading the following drawing, disclosure and claims.
The single drawing is a flow sheet showing the steps involved in a continuous process for the refining of glyceride oils according to my invention.
In the drawing, raw oil feedline 2 .and hydrocarbon solvent feed line 3 lead to mixer 4, from which outlet line 6 leads to extractor"! 'for transferring the solvent-oil niiscella' from said mixer to said extractor. Entering the top of extractor l is a feed line 8 for introducing alcoholic caustic solution and leaving the bottom of said extractor is an outlet line 9 for removing the spent caustic. Leaving the top of said extractor is an outlet line 10 for transferring the miscella to a separator l l for complete removal of the spent caustic through line l2. From said separator, a miscella outlet line [3 leads to flash distillation chamber M from which the vaporized hydrocarbon leaves an upper portion through line 16 and the refined oil leaves at the bottom through line H. Hydrocarbon vapor line l6 enters condenser 18 "from which the condensed hydrocarbon is removed through line 19 into hydrocarbon feed line -3.
Operation I have found that glyceride oils can be refined by a single treatment with an alcoholic solution of an alkali metal hydroxide. To my knowledge, it has never been tried or even realized that'the extraction and neutralization steps could be combined into a single treatment, but I have found thatglyceride oils can be efiiciently refined by such asingle treatment.
In carrying out my invention, I prefer to form a solvent-oil miscella by dissolving one part of alcohol, ethyl or isopropyl alcohol may be used instead. It is not necessary that absolute alcohol be used but the alcoholic content should be between 75 and 100 per cent, the higher water contents being desirable when operating at higher temperatures, as hereafter disclosed. I may use from 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil treated, the exact amount extraction, I prefer that the contact time be between 5 and minutes and that the temperature be between 0 and 30 0., although tempera' tures between 20 to 130" C. may be employed. K
The pressure is adjusted to maintain the reactants in the liquid phase.
lThevolume ratio of alcohol to glyceride oil should be from 0.2 1 to :1, the preferred range beingfrom 2:1 to 20:1. I
,After contact between the miscella and alcoholic caustic has been maintained for a sufficiently long time, the mixture is allowed to settle and the oily miscella is separated from the spent caustic solution. The oil and spent caustic solutions can be separated by gravity when operating under preferred conditions of high solvent to oil ratio because the miscella will be of suificiently low density, to allow the spent caustic to settle. However, when the specific gravity of the miscella and the caustic solution are more nearly equal, the separation may be made by means of a centrifuge or its equivalent.
. The paraffinic solvent added to the oil in forming the. original miscella is removed by distillation, preferably, at atmospheric pressure, the temperature vto which it must be heated, of course, being dependent on the boiling point of the solvent used. It is not desirable to heat the oil to a much higher temperature than is necessary to distill the solvent.
After such a treatment as I have just described. the refined oil will be of good color and will ordinarily contain less than 0.1 per cent of free fatty acid. The content of the break or sludge formers will be correspondingly lowered. 1
My invention may be'carried out as a batch process or the process may be continuous, as shown in the drawing. The drawing represents the apparatus adapted to carrying out a process wherein the density of miscella is suificiently below that of the caustic solution to permit countercurrent flow of liquids through the extractor. The separator, which maybe a centrifuge or any equivalent, permits more complete separation of miscella and spent caustic.
By carrying out the neutralization and alcohol extraction in a single step, the process is considerably simplified. The amount of equipment is reduced because one extractor and separator are used to carry out a treatment formerly requiringtwo reactors and two separators. This means ashorter treating cycle for refining the oil than is required in the two-stage process. Reducing theamount of equipment also reduces thecapital investment, which means an increased amount of material may be processed per unit cost. Another advantage of reduced amount of equipment is areduced amount of oil lost during processing because of leaks in equip- Sodium,
ment and oil dissolved in treating liquids. Eliminating one step of the process reduces the operating and maintenance costs.
In my process the concentration of caustic in the alcohol-caustic treating fluid is. lower than the concentration normally employed in the neutralizing fluid of a two-step process. This means less corrosion of equipment and less hydrolysis of the oil during treatment. Numerous other advantages will be apparent to those skilled in the art.
The use of mixtures of the suitable solvents and/or mixtures of the caustic materials is fully within the intended scope of my invention. My invention may be employed in the refining of innumerable oils which can be refined by caustic treatment and alcohol extraction.
The advantages of my invention will be more clearly'understood from the following examples Example I A miscella of 25.6 grams of soybean oil in grams of neohexane was treated with 100 grams of 99% methyl alcohol containing 0.04 gram of sodium hydroxide. The mixture was shaken well and allowed to separate. The two phases were separated by decanting. The oil was recovered from the hydrocarbon phase by vaporizing off the hydrocarbon at atmospheric pressure and a temperature of 60 C. A total of 25.4 grams of refined oil containing only 0.085% free fatty acid was obtained.
Example 11 A miscella containing 26.3 grams of oil in 106 grams of neohexane was heated and mixed with 100 grams of 99% methyl alcohol containing 10 ml. of a 0.1052 N-potassium hydroxide solution. The mixture was allowed to settle and the hydrocarbon phase was separated by decanting. The hydrocarbon was removed from the oil by distillation at atmospheric pressure and a temperature of 60 C. Twenty-six and four-tenths grams of refined oil was recovered. This oil was light colored and contained only 0.058% free fatty acid. (The slight excess yield of refined oil isprobably due to incomplete removal of solvent.)
The specific examples are presented to illustrate and explain the advantages of my process and are not to be considered as limiting my invention, the scope of which is defined by the following claims.
Iclaim:
1. The process of refining a glycerlde oil which comprises intimately contacting a solventoil miscella comprising a solution of said oil in from 1 to 6 volumes of a liquid hydrocarbon for a period of time from 5 to 30 minutes at a temperature of from 20 to C. with an alcoholic alkali metal hydroxide solution consisting essentially of from '75 to 100 per cent alcohol, 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil and water whenever the concentration of the alcohol employed is less than 100 per cent the ratio of alcohol to oil being from .2 to 50 volumes of said alcohol per volume of oil, separating the miscella from the caustic solution and separating the resulting miscella into the solvent and oil fractions.
2. The process for refining a glyceride oil which comprises intimately contacting a solventoil miscella comprising a solution of said oil in from 1 to 6 volumes of a liquid parailinic hydrocarbon for from 5 to 10 minutes at a temperature from 0 to 30 C. with an alcoholic alkali metal hydroxide solution consisting essentially of 75 to 100 per cent alcohol, 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil, and water whenever the concentration of the alcohol employed is less than 100 per cent, the ratio of alcohol to oil being from .2 to 50 volumes of alcohol per volume of oil, separating the miscella from the caustic solution and separating the resulting miscella into the solvent and oil fractions.
3. The process for refining a glyceride oil which comprises intimately contacting a solventoil miscella comprising a solution of said oil in from 1 to 6 volumes of a liquid parafi'inic hydrocarbon for from 5 to 10 minutes at a temperature from 0 to 30 C. with an alcoholic caustic solution containing essentially from 75 to 100 per cent alcohol, 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil, the ratio of alcohol to oil and water whenever the concentration of the alcohol employed is less than 100 per cent, being from 2 to volumes of alcohol per volume of oil, separating the miscella from the caustic solution and separating the resulting miscella into the solvent and oil fractions.
4. The process for refining a glyceride oil which comprises intimately contacting a solventoil miscella comprising a solution of said oil in from 1 to 6 volumes of a liquid paraffinic hydrocarbon for from 5 to 10 minutes at a tempera ture from 0 to C. with an alcoholic caustic solution containing essentially from 75 to 100 per cent methyl alcohol, from 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil and water whenever the concentration of the alcohol employed is less than 100 per cent, the ratio of alcohol to oil being from 2 to 20 volumes of said alcohol per volume of oil, separating the miscella from the caustic solution and separating the resulting miscella into the solvent and oil fractions.
5. The process of refining a glyceride oil which comprises intimately contacting a miscella of said oil in a liquid parafiinic solvent with a, concentrated alcoholic alkali metal hydroxide solution consisting essentially of 75-100 percent alcohol, alkali metal hydroxide, and water whenever the concentration of the alcohol employed is less than 100 percent, for a period of time sufiicient to neutralize the free fatty acids and to extract the alcohol-soluble bodies, separating the spent alcoholic caustic solution from the miscella and separating the paramnic solvent from the refined oil.
6. The process of claim 5 wherein the alcohol is methyl alcohol.
7. The process of claim 5 wherein the alcohol is ethyl alcohol.
8. The process of claim 5 wherein :the alcohol is isopropyl alcohol.
9. The process of claim 5 wherein the paramnic solvent is neohexane.
10. The process of claim 5 wherein the paraffinic solvent is n-hexane.
11. The process of claim 5 wherein the paraffinic solvent is n-pentane.
12. The process of claim 5 wherein thealkali metal hydroxide is sodium hydroxide.
13. The process of claim 5 wherein the alkali metal hydroxide is potassium hydroxide.
14. The process of refining a crude soy bean oil which comprises intimately contacting a miscella of one volume of said oil in from 4 to 6 volumes of neohexane at a temperature between 0 and 30 C. for a period of time from 5 to 10 minutes with a. to per cent methyl alcohol solution containing from 0.02 to 5 grams of alkali metal hydroxide per 100 grams of oil, separating said miscella from the spent alcoholic caustic solution and heating the separated miscella to distill the parafiinic solvent.
ARNOLD L. AYERS.
REFERENCES CITED The following references are of record in' 'the file of this patent:
UNITED STATES PATENTS Number Name Date 1,194,013 Handy et al Aug. 8, 1916 1,729,809 Wilhelm Oct. 1, 1929 2,113,942 Jones Apr. 12, 1938 2,190,590 Clayton Feb. 13, 1940 2,268,786 Dijck Jan. 6, 1942 FOREIGN PATENTS Number Country Date 252,370 Great Britain 1927 5 Great r tain Rename-a... 9 7
Claims (1)
- 5. THE PROCESS OF REFINING A GLYCERIDE OIL WHICH COMPRISES INTIMATELY CONTACTING A MISCELLA OF SAID OIL IN A LIQUID PARAFFINIC SOLVENT WITH A CONCENTRATED ALCOHOLIC ALKALI METAL HYDROXIDE SOLUTION CONSISTING ESSENTIALLY OF 75-100 PERCENT ALCOHOL, ALKALI METAL HYDROXIDE, AND WATER WHENEVER THE CONCENTRATION OF THE ALCOHOL EMPLOYED IN LESS THAN 100 PERCENT, FOR A PERIOD OF TIME SUFFICIENT TO NEUTRALIZE THE FREE FATTY ACIDS AND TO EXTRACT THE ALCOHOL-SOLUBLE BODIES, SEPARATING THE SPENT ALCOHOLIC CAUSTIC SOLUTION FROM THE MISCELLA AND SEPARATING THE PARAFFINIC SOLVENT FROM THE REFINED OIL
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US69104A US2614111A (en) | 1949-01-04 | 1949-01-04 | Process of refining glyceride oil in a liquid paraffinic solvent with a concentrated alcoholic alkali metal hydroxide solution |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| US69104A US2614111A (en) | 1949-01-04 | 1949-01-04 | Process of refining glyceride oil in a liquid paraffinic solvent with a concentrated alcoholic alkali metal hydroxide solution |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| US2614111A true US2614111A (en) | 1952-10-14 |
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| US69104A Expired - Lifetime US2614111A (en) | 1949-01-04 | 1949-01-04 | Process of refining glyceride oil in a liquid paraffinic solvent with a concentrated alcoholic alkali metal hydroxide solution |
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| US (1) | US2614111A (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2739164A (en) * | 1952-05-28 | 1956-03-20 | Sherwin Williams Co | Refining of glyceride oils |
| US2786858A (en) * | 1951-12-13 | 1957-03-26 | Extraction Continue De Smet | Method for the refining of oils and fatty substances |
| US3165540A (en) * | 1961-09-05 | 1965-01-12 | Charles F Krewson | Process for isolation of divernolin and trivernolin |
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| GB253897A (en) * | 1925-06-22 | 1926-11-04 | Ind Des Matieres Grasses Et Sa | Improvements in and relating to the neutralisation of oils and fats |
| GB252370A (en) * | 1925-05-19 | 1927-05-05 | Rocca Tassy & De Roux Ets | Improved process for neutralising oils and like fatty substances |
| US1729809A (en) * | 1927-05-02 | 1929-10-01 | Wilhelm Karl Friedrich | Process of extracting fatty acids, resins, bitter substances, and mucilage from oils and fats |
| US2113942A (en) * | 1934-06-30 | 1938-04-12 | Squibb & Sons Inc | Refining of therapeutic oils |
| US2190590A (en) * | 1937-04-05 | 1940-02-13 | Refining Inc | Process of refining glyceride oils |
| US2268786A (en) * | 1939-06-09 | 1942-01-06 | Willem Johannes Dominicu Dijck | Process for refining fatty compounds |
-
1949
- 1949-01-04 US US69104A patent/US2614111A/en not_active Expired - Lifetime
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US1194013A (en) * | 1916-08-08 | Method of refining wool-grease | ||
| GB252370A (en) * | 1925-05-19 | 1927-05-05 | Rocca Tassy & De Roux Ets | Improved process for neutralising oils and like fatty substances |
| GB253897A (en) * | 1925-06-22 | 1926-11-04 | Ind Des Matieres Grasses Et Sa | Improvements in and relating to the neutralisation of oils and fats |
| US1729809A (en) * | 1927-05-02 | 1929-10-01 | Wilhelm Karl Friedrich | Process of extracting fatty acids, resins, bitter substances, and mucilage from oils and fats |
| US2113942A (en) * | 1934-06-30 | 1938-04-12 | Squibb & Sons Inc | Refining of therapeutic oils |
| US2190590A (en) * | 1937-04-05 | 1940-02-13 | Refining Inc | Process of refining glyceride oils |
| US2268786A (en) * | 1939-06-09 | 1942-01-06 | Willem Johannes Dominicu Dijck | Process for refining fatty compounds |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US2786858A (en) * | 1951-12-13 | 1957-03-26 | Extraction Continue De Smet | Method for the refining of oils and fatty substances |
| US2739164A (en) * | 1952-05-28 | 1956-03-20 | Sherwin Williams Co | Refining of glyceride oils |
| US3165540A (en) * | 1961-09-05 | 1965-01-12 | Charles F Krewson | Process for isolation of divernolin and trivernolin |
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