US2290609A - Process for producing fatty acid polyhydric esters from glycerides - Google Patents

Process for producing fatty acid polyhydric esters from glycerides Download PDF

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US2290609A
US2290609A US356194A US35619440A US2290609A US 2290609 A US2290609 A US 2290609A US 356194 A US356194 A US 356194A US 35619440 A US35619440 A US 35619440A US 2290609 A US2290609 A US 2290609A
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fatty acid
esters
glycerides
monoesters
solvent
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Warren H Goss
Johnstone Henry Fraser
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HENRY A WALLACE
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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11C—FATTY ACIDS FROM FATS, OILS OR WAXES; CANDLES; FATS, OILS OR FATTY ACIDS BY CHEMICAL MODIFICATION OF FATS, OILS, OR FATTY ACIDS OBTAINED THEREFROM
    • C11C3/00—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom
    • C11C3/04—Fats, oils, or fatty acids by chemical modification of fats, oils, or fatty acids obtained therefrom by esterification of fats or fatty oils

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  • One object of the invention is to produce fatty acid polyhydric esters by alcoholizing fatty acid glycerides to form monoesters and diesters, separating the resulting mixture of esters into fractions by treatment with selective solvents, and converting the ester fractions thus obtained into higher polyhydric esters by alcoholysis with a polyhydric alcohol.
  • the method offers a simple and inexpensive method for separating into fractions fatty acid glycerides such as soybean oil, cottonseed oil, linseed oil, fish oils, and similar oils.
  • these oils and many others can be separated into fractions, some of which possess higher degrees of unsaturation than the original mixtures of glycerides and others which are more saturated than the original oils.
  • a second object of the invention is to provide a method for separating into fractions mixtures of fatty acid monoesters and diesters, certain of which fractions contain a higher concentration of the more unsaturated or more actively unsaturated components than the original mixture.
  • fatty acids which occur in nature as glycerides are converted into monoesters in accordance with any known methods, for example that described by Elsdon in Analyst,
  • 0 mo-(J-R' RO( ,R+CHi0HCHOH-CHzOH- Satisfactory catalysts include acids, particularly sulfom'c acids, and sodium methylate.
  • the reaction is forced toward completion by use of excess alcohol.
  • the purpose of this step in the process is to alter the mixed condition in which the fatty acids ordinarily occur in nature as glycerides, so that eflicient separation can be obtained in a subsequent step of the process.
  • monohydric alcohols such as methanol, ethanol, propanol, butanol, and amyl alcohol are preferable because of the ease with which they react with triglycerides to produce monoesters.
  • polyhydric alcohols such as ethylene glycol, glycerine, erythritol, arabitol, xylitol, mannitol, and sorbitol in this step of the process, but it is necessary to use a suiiicient excess of the alcohol to assure the formation of monoesters and diesters
  • the reaction is carried out by heating together the glycerides and alcohol with the catalyst. When equal volumes of soybean oil and methanol are heated together with 0.3 percent of sodium methylate based upon the weight of oil, the reaction goes substantially to completion during the time ordinarily required to heat the mixture to boiling and to cool it to room temperature.
  • the mixtures of monoesters or diesters may be fractionated by liquid-liquid extraction without removing the excess alcohols remaining after the alcoholysis, but it is usually preferable to separate the alcohols and' esters. This can be accomplished by any known methods, for example by washing the mixture with water, in the cases of water-soluble alcohols.
  • the aqueous washings can be fractionally distilled in order to recover the alcohols which can be returned to the system. After removal of the excess alcohol the esters may. if desirable, be fractionally distilled before being subjected to selective solvent fractionation.
  • selective solvent action is defined as the. ability of solvents and combinations of solvents to separate dissolved materials by virtue of chemical or physical afiinity of said solvents for certain relatively active groupings which occur in the dissolved molecules.
  • Relatively active groupings are those which contribute to the ability of polyhydric fatty acid esters to form suitable drying films through polymerization and oxidation. Examples of such groupings include unsaturated double bonds and conjugated unsaturated double bonds. For example, we have found that furfural possesses a greater solvent power for unsaturated fatty acid monoesters than for the more saturated fatty acid monoesters.
  • hydrocarbons such as hexane and benzene are excellent solvents for both saturated and unsaturated monoesters of fatty acids. Since hexane and furfural are only slightly miscible at room temperatures, a mixture of monoesters of fatty acids possessing varying degrees of unsaturation will distribute itself between a mixture of hexane and furfural in such a way that th esters contained in the furfural-rich phase possess a higher degree of unsaturation than does that portion of the ester mixture which dissolves in the hexane-rich phase.
  • Example 1.'Io illustrate the fractionation step in our process, 47.5 grams of the mixed ethyl esters derived from soybean oil was thoroughly agitated with 116 grams of furfural and 32 grams of a commercial grade of mixed pentanes and hexanes, at F. The esters were then. recovered from each of the two liquid layers. Of the esters thus recovered, 29 percent was in the lower or furfural-rich layer, and when the solvent was removed this fraction had an iodine value of 130.1. The. upper or hydrocarbon-rich layer contained the other 71 percent of the original esters which, when the solvent was removed, had an iodine value of 118.3. The iodine value of the original mixture of esters was 121.8.
  • Example 2 In a similar experiment, 47.5 grams of the above-described ethyl esters of soybean acids was mixed with 116 grams of furfural and 575 grams of the hydrocarbon solvent. Approximately 2 percent of the recovered esters was in the furfural-rich layer and possessed an io-- rich layer, approximately 141 grams of esters having an iodine value of 120.8.
  • Example 4.-At 85 F. a mixture of 712 grams of the above-mentioned monoesters, 1,160 grams of furfural, and 1,600 grams of pentanes and hexanes was separated and yielded, from the furfural-rich layer, 5.1 percent of the original esters having an iodine value of 137.0. The remaining 94.9 percent of the esters remained in the hydrocarbon-rich layer and possessed, an iodine value of 120.8.
  • the extract layer, or furfural-rich layer was further extracted with 980 grams of fresh hydrocarbon solvent. The new extract layer contained 7.7 percent of the esters which remained in the first extract layer and had an iodine value of 146.3. The remaining 92.3 percent of the first extract was recovered from the rafiinate layer and possessed an iodine value of 136.3.
  • Soybean oil may be separated into two frac- 75 tions, the separation being accomplished by furfural extraction of a hexane solution of methyl esters of the fatty acids derived from the soybean oil.
  • Methanol and soybean oil are heated in the presence of a catalyst in a reaction kettle, and after the reaction is substantially complete, the glycerine produced and the excess of methanol are washed out of the resulting mixture of fatty acid methyl esters by means of water.
  • the washings are subsequently fractionally distilled in a recovery system to reclaim the methanol and glycerine which are returned to the system.
  • the methyl esters are passed through a vacuum drier where final traces of moisture are removed.
  • the palmitic acid esters may be separated from the esters of stearic, oleic, linoleic, and linolenic acids.
  • the combination of fractional distillation with selective solvent extraction therefore affords a convenient and efiicient means for controlling both the chain length and the degree of unsaturation in the acyl radicals which compose the ultimate products.
  • the methyl esters are dissolved in hexane and countercurrently extracted with furfural.
  • the raflinate layer leaves the column near the top and consists of a hexane solution of relatively saturated methyl esters along with small amounts of furfural.
  • the extract layer is removed from the bottom of the column and consists of a furfural solution of relatively unsaturated monoesters along with small amounts of hexane.
  • the raflinate-and extract layers are treated in separate fractional distillation columns, the furfural and hexane being distilled, condensed, and returned to the extraction column.
  • the glycerides produced in one reaction kettle have a much lower iodine value than the vegetable oil shortenings, margarine, lar edible products.
  • the glycerides produced in the other reaction kettle have a very high iodine value and possess bodying and drying properties which make them much and simimore valuable than the original soybean oil for varnishes, paints,
  • soybean oil by subjecting the oil itself to the action of selective solvents.
  • This method is subject to severe limitations imposed by the mixed condition in which the glycerides are synthesized in nature.
  • a consideration of the amounts of the various acids present in soybean oil glycerides reveals that the only single acid present in sufficient quantity to permit the existence of appreciable amounts of its triglyceride is linoleic acid.
  • the amounts of trilinolenin, triolein, tristearin, and tripalmitin present in soybean oil appear to be so small that, for most practical purposes, their presence is negligible.
  • soybean oil can contain very little glyceride material having an iodine value greater than 1'73, which is the theoretical value for trilinolein. It appears that between 30 and 40 percent of the glycerides in soybean oil are either trilinolein or glycerides having an equivalent number of double bonds and, accordingly, the same iodine value as trilinolein.
  • the latter type of glyceride is exemplifled by the glyceride molecule which contains one each of oleic, linoleic, and linolenic acid radicals.
  • Soybean oil contains little glyceride material possessing an iodine value lower than 88 which is the theoretical value of triolein. Although substantially no present in soybean oil, it appears that approximately 35 to 50 percent of a typical soybean oil is present as glycerides having the same number of double bonds as triolein. This glyceride material consists, for the most part, of glyceride molecules containing one each of linoleic, oleic, and saturated fatty acid radicals.
  • triolein is The method which we propose completely avoids fractionation difficulties caused by the mixed condition in which the fatty acids occur as glycerides, and it provides an efficient and convenient method of separating glycerides more effectively than can be accomplished by extraction of the glycerides themselves.
  • a method of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid ester linkages per molecule which consists of alcoholysis of the glycerides thereby producing fatty acid esters having less than three fatty acid ester linkaae eoe ages per molecule, thence fractionating the esters resulting from said alcoholysis by means of a solvent system wherein the esters are distributed between incompletely miscible liquid phases, thence separating the phases, and subjecting the ester fractions contained therein to alcoholysis by means of a polyhydric alcohol having. at least three hydroxy groups.
  • a method of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid ester linkages per molecule which consists of alcoholysis of the glycerides by means of a polyhydric alcohol thereby producing fatty acid monoesters of the polyhydric alcohol, thence fractionating the monoesters by means of a solvent system wherein the esters are distributed between incompletely miscible liquid phases, thence separating the phases, and thence alcoholizihg the ester fractions contained therein by means of a polyhydric alcohol having at least three hydroxy groups.
  • Amethod of selectively separating mixtures of fatty acid esters having less than three fatty acid ester linkages per molecule into fractions, one of which contains a high concentration of relatively active groupings and another which contains a lesser concentration of such groupings which consists of treating the mixture of esters with a solvent system wherein the esters are distributed between incompletely miscible liquid phases, separating the phases, and removing the solvent system.
  • a method of selectively separating fatty acid monoesters into fractions, one of which contains a high concentration of relatively unsaturated valence bonds and another which contains a lesser concentration of unsaturated valence bonds which consists of treating the monoesters with a solvent system wherein the monoesters are distributed between incompletely miscible liquid phases, separating the phases, and removing the solvent system.
  • a method of selectively separating fatty acid monoesters into fractions, one of which contains a high concentration of relatively-unsaturated valencc bonds and another which contains a lesser concentration of unsaturated valence bonds which consists of treating said fatty acid monoesters with liquids, one of which possess a greater aifinity for unsaturated groupings than does the other, separating the two liquid phases, and removing the solvents.
  • a method of selectively separating fatty acid monoesters into fractions, one of which contains a high concentration of unsaturated valence bonds and another which contains a lesser concentration of unsaturated valence bonds which consists of treating said fatty acid monoesters with a solvent under conditions in which incomplete miscibility exists, separating the resulting liquid phases, and removing the solvents.

Description

Patented July 21, 1942 UNITED STATES PATENT OFFICE PROCESS FOR PRODUCING FATTY ACID POLYHYDRIC ESTERS FROM GLYCERIDES Warren H. Goss, Cham J ohnstone, Urbana,
paign, and Henry Fraser 111., assignors to Henry A.
Wallace, as Secretary of Agriculture 01? the United States of America, and to his successors No Drawing. Application September 10, 1940, Serial No. 356,194
(01. 260-411) (Granted under the act 32 Claims.
amended April 30, 19
tures thereof in conjunction with processes of alcoholysis to produce, from glyceride oils, fatty acid polyhydric esters having enhanced value for industrial and food uses.
One object of the invention is to produce fatty acid polyhydric esters by alcoholizing fatty acid glycerides to form monoesters and diesters, separating the resulting mixture of esters into fractions by treatment with selective solvents, and converting the ester fractions thus obtained into higher polyhydric esters by alcoholysis with a polyhydric alcohol. For example, the method offers a simple and inexpensive method for separating into fractions fatty acid glycerides such as soybean oil, cottonseed oil, linseed oil, fish oils, and similar oils. By application of this invention, these oils and many others can be separated into fractions, some of which possess higher degrees of unsaturation than the original mixtures of glycerides and others which are more saturated than the original oils.
A second object of the invention is to provide a method for separating into fractions mixtures of fatty acid monoesters and diesters, certain of which fractions contain a higher concentration of the more unsaturated or more actively unsaturated components than the original mixture.
Although the examples cited herein are restricted to soybean oil, our experiments show that the process is applicable to fats and oils in general, such as soybean oil, linseed oil, cottonseed oil, fish oils, coconut oil, tung oil, castor oil, rapeseed oil, and similar oils.
In our invention the fatty acids which occur in nature as glycerides are converted into monoesters in accordance with any known methods, for example that described by Elsdon in Analyst,
of March 3, 1883, as 28;-370 0. G. 757) 38, 8-11 (1913), wherein fatty acid glycerides are treated, in the presence of a catalyst, with a. quantity of alcohol substantially in excess of that quantity required to alcoholize the fatty acids stoichiometrically into monoesters, thus:
0 mo-(J-R' RO( ,R+CHi0HCHOH-CHzOH- Satisfactory catalysts include acids, particularly sulfom'c acids, and sodium methylate. The reaction is forced toward completion by use of excess alcohol. The purpose of this step in the process is to alter the mixed condition in which the fatty acids ordinarily occur in nature as glycerides, so that eflicient separation can be obtained in a subsequent step of the process.
In most cases, monohydric alcohols such as methanol, ethanol, propanol, butanol, and amyl alcohol are preferable because of the ease with which they react with triglycerides to produce monoesters. It is also possible to use polyhydric alcohols such as ethylene glycol, glycerine, erythritol, arabitol, xylitol, mannitol, and sorbitol in this step of the process, but it is necessary to use a suiiicient excess of the alcohol to assure the formation of monoesters and diesters The reaction is carried out by heating together the glycerides and alcohol with the catalyst. When equal volumes of soybean oil and methanol are heated together with 0.3 percent of sodium methylate based upon the weight of oil, the reaction goes substantially to completion during the time ordinarily required to heat the mixture to boiling and to cool it to room temperature.
The mixtures of monoesters or diesters may be fractionated by liquid-liquid extraction without removing the excess alcohols remaining after the alcoholysis, but it is usually preferable to separate the alcohols and' esters. This can be accomplished by any known methods, for example by washing the mixture with water, in the cases of water-soluble alcohols. The aqueous washings can be fractionally distilled in order to recover the alcohols which can be returned to the system. After removal of the excess alcohol the esters may. if desirable, be fractionally distilled before being subjected to selective solvent fractionation.
The term selective solvent action as herein used is defined as the. ability of solvents and combinations of solvents to separate dissolved materials by virtue of chemical or physical afiinity of said solvents for certain relatively active groupings which occur in the dissolved molecules. Relatively active groupings are those which contribute to the ability of polyhydric fatty acid esters to form suitable drying films through polymerization and oxidation. Examples of such groupings include unsaturated double bonds and conjugated unsaturated double bonds. For example, we have found that furfural possesses a greater solvent power for unsaturated fatty acid monoesters than for the more saturated fatty acid monoesters. On the other hand, hydrocarbons such as hexane and benzene are excellent solvents for both saturated and unsaturated monoesters of fatty acids. Since hexane and furfural are only slightly miscible at room temperatures, a mixture of monoesters of fatty acids possessing varying degrees of unsaturation will distribute itself between a mixture of hexane and furfural in such a way that th esters contained in the furfural-rich phase possess a higher degree of unsaturation than does that portion of the ester mixture which dissolves in the hexane-rich phase.
The separation of glyceride fats and oils into fractions by means of solvents with which the glycerides are only partially miscible has been described by Bills in the Journal of Biological Chemistry, 67, 279-285 (1926). A number of the solvents described in this publication as exhibiting incomplete miscibility with glycerides are listed in Table I.
Table I Furfural Ethyl lactate Nitromethane Formamide Acetic acid Ethyl acetoacetate Furfuryl alcohol Glycerine Ethylene chlorohydrin Monoacetin Methyl alcohol Diacetin Ethyl alcohol Triacetin' Ethanolamine Ethyl sulfate. Ethylene glycol Methyl sulfate Allyl alcohol Pyruvic acid We have found that solvents such as those listed in Table I which possessselective solvent properties for various types of glycerides also exhibit a selective solvent action toward fatty acid monoesters. However, we have further found that many of the usual selective solvents such as furfural, furfuryl alcohol, and ethylene glycol monomethyl ether are completely miscible with monoesters of fatty acids in the temperature ranges in which partial miscibility is observed between the solvents and glycerides of fatty acids. It is therefore advisable to employ a second solvent which is incompletely miscible with the selective solvent but which is miscible with the fatty acid esters. The operation, in this case, results in a distribution of the esters between the two solvent layers in such a way that the esters contained in the respective layers possess different degrees of unsaturation. In some cases, the use of asecond solvent can be avoided by adding water to the selective solvent fatty acid esters.
Additional solvents which can be used in the fractionation step of our process are listed in Table II, but our process is operable using any of a large number of solvents of which those listed in Tables I and II are only examples.
Table II Ethylene glycol monomethyl ether Sulfur dioxide Dichlorodiethyl ether Tetrahydrofurfuryl alcohol Methyl formate Methyl lactate Acetamide Acetonitrile Diacetone Ethyl oxalate Acetaldehyde When itis desired toemploy a second solvent in this step of the process, hydrocarbons, such as hexane, cetane, and benzene are satisfactory in most cases, although any liquid which is not completely miscible with the particular selective solvent used and which possesses the required solubility for fatty acid esters is also suitable. For example,. Chlorex (dichlorodiethyl ether), although completely miscible with glyceride oils and with the corresponding fatty acid monoesters, can be employed in conjunction with a hydrocarbon to fractionate fatty acid monoesters.
The particular temperatures and solvent ratios to be used in the extraction equipment depend upon the equilibrium relationships of the particular system chosen. Examples of satisfactory operating temperatures and solvent ratios for furfural-hydrocarbon and. methyl cellosolvehydrocarbon systems for the extraction of ethyl esters of soybean acids are described in the following examples:
Example 1.'Io illustrate the fractionation step in our process, 47.5 grams of the mixed ethyl esters derived from soybean oil was thoroughly agitated with 116 grams of furfural and 32 grams of a commercial grade of mixed pentanes and hexanes, at F. The esters were then. recovered from each of the two liquid layers. Of the esters thus recovered, 29 percent was in the lower or furfural-rich layer, and when the solvent was removed this fraction had an iodine value of 130.1. The. upper or hydrocarbon-rich layer contained the other 71 percent of the original esters which, when the solvent was removed, had an iodine value of 118.3. The iodine value of the original mixture of esters was 121.8.
Example 2.In a similar experiment, 47.5 grams of the above-described ethyl esters of soybean acids was mixed with 116 grams of furfural and 575 grams of the hydrocarbon solvent. Approximately 2 percent of the recovered esters was in the furfural-rich layer and possessed an io-- rich layer, approximately 141 grams of esters having an iodine value of 120.8.
Example 4.-At 85 F., a mixture of 712 grams of the above-mentioned monoesters, 1,160 grams of furfural, and 1,600 grams of pentanes and hexanes was separated and yielded, from the furfural-rich layer, 5.1 percent of the original esters having an iodine value of 137.0. The remaining 94.9 percent of the esters remained in the hydrocarbon-rich layer and possessed, an iodine value of 120.8. The extract layer, or furfural-rich layer, was further extracted with 980 grams of fresh hydrocarbon solvent. The new extract layer contained 7.7 percent of the esters which remained in the first extract layer and had an iodine value of 146.3. The remaining 92.3 percent of the first extract was recovered from the rafiinate layer and possessed an iodine value of 136.3.
The foregoing are examples of batch operation. Much more efficient separation and insecured in the liquid-liquid extraction step of the process by use of an apparatus for carrying it out on a continuous, countercurrent scale. This may consist of any of the numerous devices in common use for securing intimate contact between immiscible liquids in countercurrent flow and subsequently 40 After the extraction process, the solvents may and xylitol. follows:
HO("3R+3ROH o H2O(%R This reaction is carried out in apparatus and under conditions which are similar to those employed in the initial alcoholysis step of our process, but it is necessary to operate under conditions which permit the removal of alcohol formed by the reaction in order to force the reaction toward completion. The removal of the alcohol produced is effected, for example, by carrying out the reaction at a temperature at which the alcohol may be distilled as it is produced. Since this reaction is substantially the reverse of the initial alcoholysis step in our process, the same catalysts are effective.
Soybean oil may be separated into two frac- 75 tions, the separation being accomplished by furfural extraction of a hexane solution of methyl esters of the fatty acids derived from the soybean oil. Methanol and soybean oil are heated in the presence of a catalyst in a reaction kettle, and after the reaction is substantially complete, the glycerine produced and the excess of methanol are washed out of the resulting mixture of fatty acid methyl esters by means of water. The washings are subsequently fractionally distilled in a recovery system to reclaim the methanol and glycerine which are returned to the system. The methyl esters are passed through a vacuum drier where final traces of moisture are removed.
In many cases it is advantageous to distill the monoesters, but is possible to omit the still and to feed the dried methyl esters directly to the extraction column. The use of the still is often desirable in order to increase the purity of the and it is also possible to design such apparatus to effect a separation of the monoesters into fractions having different fatty acid chain lengths. For example, the palmitic acid esters may be separated from the esters of stearic, oleic, linoleic, and linolenic acids. The combination of fractional distillation with selective solvent extraction therefore affords a convenient and efiicient means for controlling both the chain length and the degree of unsaturation in the acyl radicals which compose the ultimate products.
In the extraction column the methyl esters are dissolved in hexane and countercurrently extracted with furfural. The raflinate layer leaves the column near the top and consists of a hexane solution of relatively saturated methyl esters along with small amounts of furfural. The extract layer is removed from the bottom of the column and consists of a furfural solution of relatively unsaturated monoesters along with small amounts of hexane. The raflinate-and extract layers are treated in separate fractional distillation columns, the furfural and hexane being distilled, condensed, and returned to the extraction column.
The fractions of monoesters obtained from the rafiinate and extract layers pass to separate reaction kettles in which they catalytically react with stoichiometric amounts ofglycerine obtained from the glycerine recovery system. In order to bring this reaction to completion, the methanol generated by the reaction is distilled from the resulting glycerides and returned to the methanolysis reaction kettle. 1
The glycerides produced in one reaction kettle have a much lower iodine value than the vegetable oil shortenings, margarine, lar edible products. The glycerides produced in the other reaction kettle, on the other hand, have a very high iodine value and possess bodying and drying properties which make them much and simimore valuable than the original soybean oil for varnishes, paints,
ring in an oil such as soybean oil by subjecting the oil itself to the action of selective solvents. By such a process, it is possible to split soybean oil into fractions containing, on the one hand, glycerides of relatively highly unsaturated fatty acids and, on the other hand, glycerides composed of the more saturated acids. This method, however, is subject to severe limitations imposed by the mixed condition in which the glycerides are synthesized in nature. For example, a consideration of the amounts of the various acids present in soybean oil glycerides reveals that the only single acid present in sufficient quantity to permit the existence of appreciable amounts of its triglyceride is linoleic acid. The amounts of trilinolenin, triolein, tristearin, and tripalmitin present in soybean oil appear to be so small that, for most practical purposes, their presence is negligible.
Consideration of the work of Hilditch as described in the Journal of the Society of Chemical Industry, 53T, 13-21 (1934) indicates that soybean oil can contain very little glyceride material having an iodine value greater than 1'73, which is the theoretical value for trilinolein. It appears that between 30 and 40 percent of the glycerides in soybean oil are either trilinolein or glycerides having an equivalent number of double bonds and, accordingly, the same iodine value as trilinolein. The latter type of glyceride is exemplifled by the glyceride molecule which contains one each of oleic, linoleic, and linolenic acid radicals.
Soybean oil, on the other hand, contains little glyceride material possessing an iodine value lower than 88 which is the theoretical value of triolein. Although substantially no present in soybean oil, it appears that approximately 35 to 50 percent of a typical soybean oil is present as glycerides having the same number of double bonds as triolein. This glyceride material consists, for the most part, of glyceride molecules containing one each of linoleic, oleic, and saturated fatty acid radicals.
These considerations impose definite limitations both upon the degree of unsaturation and upon the yields which are theoretically obtainable by subjecting soybean oil glycerides to the action of selective solvents. Furthermore, carrying out a selective solvent extraction upon soybean oil glycerides by means of an immiscible solvent or combination of solvents presents numerous practical difficulties which still further restrict the yields and degrees of unsaturation attainable in the end products.
triolein is The method which we propose completely avoids fractionation difficulties caused by the mixed condition in which the fatty acids occur as glycerides, and it provides an efficient and convenient method of separating glycerides more effectively than can be accomplished by extraction of the glycerides themselves.
The foregoing examples are to be considered only as illustrations of the proposed process, and numerous modifications may be made therein without departure from the spirit of the invention or the scope of the following claims.
Having thus described our invention, what we claim for Letters Patent is:
l. A method of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid ester linkages per molecule which consists of alcoholysis of the glycerides thereby producing fatty acid esters having less than three fatty acid ester linkaae eoe ages per molecule, thence fractionating the esters resulting from said alcoholysis by means of a solvent system wherein the esters are distributed between incompletely miscible liquid phases, thence separating the phases, and subjecting the ester fractions contained therein to alcoholysis by means of a polyhydric alcohol having. at least three hydroxy groups.
2. A method of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid'ester linkages per molecule which consists of alcoholysis of the glycerides by a monohydric alcohol, thence fractionating the esters resulting from said alcoholysis by means of a solvent system wherein the esters are distributed between incompletely miscible liquid phases, thence separating the phases, and thence subjecting the ester fractions contained therein to alcoholysis by means of a polyhydric alcohol having at least three hydroxy groups.
3. A method of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid ester linkages per molecule, which consists of alcoholysis of the glycerides by means of a polyhydric alcohol thereby producing fatty acid monoesters of the polyhydric alcohol, thence fractionating the monoesters by means of a solvent system wherein the esters are distributed between incompletely miscible liquid phases, thence separating the phases, and thence alcoholizihg the ester fractions contained therein by means of a polyhydric alcohol having at least three hydroxy groups.
4. A process of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid ester linkages per molecule, which consists of alcoholysis of the glycerides, thereby producing fatty acid esters having less than three fatty acid ester linkages per molecule, thence separating the esters resulting from said alcoholysis into fractions, one of which contains a higher concentration of unsaturated valence bonds and another of which contains a lesser concentration of unsaturated valence bonds, said fractionation being effected by treating the esters with a solvent system wherein the esters are distributed between incompletely miscible liquid phases, thence separating the phases, and thence subjecting their respective contents of fatty acid esters to alcoholysis with polyhydric alcohols having at least three hydroxy groups.
5. A process as defined in claim 1 in which the fatty acid glycerides are soybean oil.
6. A process as defined in claim 1 in which the fatty acid glycerides are cottonseed oil.
'7. A process as defined in claim 1 in which the fatty acid glycerides are linseed oil.
8. A process of converting fatty acid glycerides into fractions of fatty acid polyhydric esters having at least three fatty acid ester linkages per molecule which consist of alcoholysis of the glycerides, thereby producing fatty acid esters having less than three fatty acid ester linkages per molecule, thence fractionating the esters resulting from said alcoholysis by means of a solvent system wherein the esters are distributed between incompletely miscible phases, said solvent system consisting of a singlesolvent which is incompletely miscible with the esters, thence separating the phases, and thence subjecting the 9. A process of converting fatty acid glycerides into fractions of fatty acid polyhydrlc esters having at least three fatty acid ester linkages per molecule, which consists of alcoholysis of the glycerides, thereby producing fatty acid esters having less than three fatty acid ester linkages per molecule, thence fractionating the esters resulting from said alcoholysis by means of a solvent system wherein the esters are distributed between incompletely miscible phases, said solvent system consisting of two incompletely miscible liquids between which the fatty acid esters are distributed in accordance with their solubilities in the respective solvents, thenceseparating the respective solvent phases from each other, and thence subjecting the ester fractions contained therein to alcoholysis by means of a polyhydric alcohol having at least three hydroxy groups.
10. A process as defined in claim 8 in which the solvent is furfural containing less than percent of dissolved water.
11. A process as defined in claim 8 in which the solvent is ethylene glycol monomethyl ether containing less than 5 percent of dissolved water.
12. A process as defined in claim 8 in which the solvent is ttrahydrofurfuryl alcohol containing less than 10 percent of dissolved water.
3. A process as defined in claim 9 in which the two immiscible liquids are furfural and a hydrocarbon.
14. A proces as defined in claim 9 in which the two immiscible liquids are ethylene glycol monomethyl ether and a hydrocarbon.
15. A process as defined in claim 9 in which the two immiscible liquids are dichlorodiethyl ether and a hydrocarbo 16. A process as defined in claim 1 in which the initial alcoholysis is performed with methyl alcohol.
17. A proces as defined in claim 1 in which the initial alcoholysisis performed with ethyl alcohol.
18. A process as defined in claim 1 in which the initial alcoholysis is performed with propyl alcohol.
19. A process as defined in claim 1 in which tllifilfinal alcoholysis i accomplished using glyce e.
20. A process as defined in claim 1 in which 3: lfinal alcoholysis is accomplished using man- 21. A process as defined in claim 1 in which the final alcoholysis is accomplished using sorbltol.
22. A process as defined in claim 4 in which the unsaturated valence bonds are in the nonconjugated position.
23. A process as defined in claim 4 in which the unsaturated double bonds are in the con jugated position.
24. A process for selectively separating glyceride fats and oils into fractions, one of which is more highly unsaturated and another of which is more highly saturated than the original glycerides, which consists of alcoholysis of the glycerides to produce fatty acid monoesters, fractionating the monoesters with a solvent system consisting of a pair of incompletely miscible liquids between which the esters are distributed, separating the resulting liquid phases, and subjecting the respective fractions of esters to alcoholysis by means of glycerine, thereby producing fatty acid triglycerides.
25. Amethod of selectively separating mixtures of fatty acid esters having less than three fatty acid ester linkages per molecule into fractions, one of which contains a high concentration of relatively active groupings and another which contains a lesser concentration of such groupings, which consists of treating the mixture of esters with a solvent system wherein the esters are distributed between incompletely miscible liquid phases, separating the phases, and removing the solvent system.
26. A method of selectively separating fatty acid monoesters into fractions, one of which contains a high concentration of relatively unsaturated valence bonds and another which contains a lesser concentration of unsaturated valence bonds, which consists of treating the monoesters with a solvent system wherein the monoesters are distributed between incompletely miscible liquid phases, separating the phases, and removing the solvent system.
27. A method of selectively separating fatty acid monoesters into fractions, one of which contains a high concentration of relatively-unsaturated valencc bonds and another which contains a lesser concentration of unsaturated valence bonds, which consists of treating said fatty acid monoesters with liquids, one of which possess a greater aifinity for unsaturated groupings than does the other, separating the two liquid phases, and removing the solvents.
28. A method of selectively separating fatty acid monoesters into fractions, one of which contains a high concentration of unsaturated valence bonds and another which contains a lesser concentration of unsaturated valence bonds, which consists of treating said fatty acid monoesters with a solvent under conditions in which incomplete miscibility exists, separating the resulting liquid phases, and removing the solvents.
29. A process as defined in claim 28 in which immiscibility is obtained by addition of water.
30. A process as defined in claim 27 in which the pair of incompletely miscible liquids consists of furfural and a hydrocarbon.
31. A process as defined in claim 27 in which the pair of incompletely miscible liquids consists of dichlorodiethyl ether and a hydrocarbon.
32. A process as defined in claim 2'7 in which the pair of incompletely miscible liquids consists of a nitroparafiin and a hydrocarbon.
WARREN H. GOSS. HENRY FRASER JOHNSTONE.
a pair of incompletely miscible
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Cited By (24)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2442531A (en) * 1944-11-06 1948-06-01 Procter & Gamble Process for treating fats and fatty oils
US2442532A (en) * 1945-11-13 1948-06-01 Procter & Gamble Treatment of glycerides for use in edible fats
US2447186A (en) * 1945-01-01 1948-08-17 Photo Technical Corp Producing lower alkyl esters
US2469371A (en) * 1946-08-14 1949-05-10 Baker Castor Oil Co Process of reacting glyceride oils
US2543421A (en) * 1942-11-03 1951-02-27 Nopco Chem Co Transesterification process
US2576841A (en) * 1946-01-17 1951-11-27 Swift & Co Solvent fractionation
US2588435A (en) * 1942-06-19 1952-03-11 Lever Brothers Ltd Process of treating fatty material
US2651646A (en) * 1950-03-04 1953-09-08 Colgate Palmolive Peet Co Liquid-liquid extraction process
US2759954A (en) * 1949-02-02 1956-08-21 Chemical Foundation Inc Refining crude fatty acid monoglyceride
US3051734A (en) * 1959-11-23 1962-08-28 Sol B Radlove Method of making diglycerides
US3082228A (en) * 1959-12-18 1963-03-19 Escambia Chem Corp Method for producing monoesters of polyunsaturated fatty acids
US4164506A (en) * 1977-03-17 1979-08-14 Kao Soap Co., Ltd. Process for producing lower alcohol esters of fatty acids
US4360694A (en) * 1980-04-09 1982-11-23 Ksv-Chemicals Oy Process for preparing 1,2-diacyl-sn-glycerols
US5288619A (en) * 1989-12-18 1994-02-22 Kraft General Foods, Inc. Enzymatic method for preparing transesterified oils
US5491226A (en) * 1994-04-06 1996-02-13 Procter & Gamble Company Process for preparing polyol polyesters having low levels of triglycerides
US5885946A (en) * 1994-09-07 1999-03-23 Raision Tehtaat Oy Ab Process for preparing a synthetic ester from a vegetable oil
US6965044B1 (en) 2001-07-06 2005-11-15 Iowa State University Research Foundation Method of converting free fatty acids to fatty acid methyl esters with small excess of methanol
US20070277429A1 (en) * 2003-01-27 2007-12-06 Jackam John P Production of biodiesel and glycerin from high free fatty acid feedstocks
US20070277430A1 (en) * 2003-01-27 2007-12-06 Jackman John P Production of biodiesel and glycerin from high free fatty acid feedstocks
US20070277432A1 (en) * 2003-01-27 2007-12-06 Nova Biosource Technologies, Llc Production of biodiesel and glycerin from high free fatty acid feedstocks
US8497389B2 (en) 2008-12-08 2013-07-30 Initio Fuels Llc Single step transesterification of biodiesel feedstock using a gaseous catalyst
US9328054B1 (en) 2013-09-27 2016-05-03 Travis Danner Method of alcoholisis of fatty acids and fatty acid gyicerides
US9725397B2 (en) 2003-01-27 2017-08-08 REG Seneca, LLC Production of biodiesel and glycerin from high free fatty acid feedstocks
US9957464B2 (en) 2013-06-11 2018-05-01 Renewable Energy Group, Inc. Methods and devices for producing biodiesel and products obtained therefrom

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2588435A (en) * 1942-06-19 1952-03-11 Lever Brothers Ltd Process of treating fatty material
US2543421A (en) * 1942-11-03 1951-02-27 Nopco Chem Co Transesterification process
US2442531A (en) * 1944-11-06 1948-06-01 Procter & Gamble Process for treating fats and fatty oils
US2447186A (en) * 1945-01-01 1948-08-17 Photo Technical Corp Producing lower alkyl esters
US2442532A (en) * 1945-11-13 1948-06-01 Procter & Gamble Treatment of glycerides for use in edible fats
US2576841A (en) * 1946-01-17 1951-11-27 Swift & Co Solvent fractionation
US2469371A (en) * 1946-08-14 1949-05-10 Baker Castor Oil Co Process of reacting glyceride oils
US2759954A (en) * 1949-02-02 1956-08-21 Chemical Foundation Inc Refining crude fatty acid monoglyceride
US2651646A (en) * 1950-03-04 1953-09-08 Colgate Palmolive Peet Co Liquid-liquid extraction process
US3051734A (en) * 1959-11-23 1962-08-28 Sol B Radlove Method of making diglycerides
US3082228A (en) * 1959-12-18 1963-03-19 Escambia Chem Corp Method for producing monoesters of polyunsaturated fatty acids
US4164506A (en) * 1977-03-17 1979-08-14 Kao Soap Co., Ltd. Process for producing lower alcohol esters of fatty acids
US4360694A (en) * 1980-04-09 1982-11-23 Ksv-Chemicals Oy Process for preparing 1,2-diacyl-sn-glycerols
US5288619A (en) * 1989-12-18 1994-02-22 Kraft General Foods, Inc. Enzymatic method for preparing transesterified oils
US5491226A (en) * 1994-04-06 1996-02-13 Procter & Gamble Company Process for preparing polyol polyesters having low levels of triglycerides
US5885946A (en) * 1994-09-07 1999-03-23 Raision Tehtaat Oy Ab Process for preparing a synthetic ester from a vegetable oil
US6965044B1 (en) 2001-07-06 2005-11-15 Iowa State University Research Foundation Method of converting free fatty acids to fatty acid methyl esters with small excess of methanol
US7871448B2 (en) 2003-01-27 2011-01-18 Seneca Landlord, Llc Production of biodiesel and glycerin from high free fatty acid feedstocks
US20070277430A1 (en) * 2003-01-27 2007-12-06 Jackman John P Production of biodiesel and glycerin from high free fatty acid feedstocks
US20070277432A1 (en) * 2003-01-27 2007-12-06 Nova Biosource Technologies, Llc Production of biodiesel and glycerin from high free fatty acid feedstocks
US7806945B2 (en) 2003-01-27 2010-10-05 Seneca Landlord, Llc Production of biodiesel and glycerin from high free fatty acid feedstocks
US20070277429A1 (en) * 2003-01-27 2007-12-06 Jackam John P Production of biodiesel and glycerin from high free fatty acid feedstocks
US8088183B2 (en) 2003-01-27 2012-01-03 Seneca Landlord, Llc Production of biodiesel and glycerin from high free fatty acid feedstocks
US8728177B2 (en) 2003-01-27 2014-05-20 Seneca Landlord, L.L.C. Production of biodiesel and glycerin from high free fatty acid feedstocks
US9725397B2 (en) 2003-01-27 2017-08-08 REG Seneca, LLC Production of biodiesel and glycerin from high free fatty acid feedstocks
US8497389B2 (en) 2008-12-08 2013-07-30 Initio Fuels Llc Single step transesterification of biodiesel feedstock using a gaseous catalyst
US9957464B2 (en) 2013-06-11 2018-05-01 Renewable Energy Group, Inc. Methods and devices for producing biodiesel and products obtained therefrom
US10450533B2 (en) 2013-06-11 2019-10-22 Renewable Energy Group, Inc. Methods and devices for producing biodiesel and products obtained therefrom
US9328054B1 (en) 2013-09-27 2016-05-03 Travis Danner Method of alcoholisis of fatty acids and fatty acid gyicerides

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