JP2010215896A - Method for purifying and producing vegetable oil - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide a method for efficiently reducing and eliminating a phosphorus compound and a sterol glycoside included in a vegetable oil as impurities from the vegetable oil. <P>SOLUTION: A method for purifying and producing the vegetable oil includes: step 1 of adding one or more kinds of non-phosphorus surfactants, which are selected from among an anionic surfactant, a cationic surfactant and an amphoteric surfactant, or a solution of the same to the vegetable oil containing a sterol glycoside and a phosphorus compound and mixing by stirring to give a mixture; step 2 of further adding a definite amount of water to the mixture obtained in step 1 and mixing by stirring to give a mixture containing an aggregate; and step 3 of separating the aggregate from the mixture obtained in step 2 to give the vegetable oil from which the sterol glycoside and the phosphorus compound have been removed each at a ratio of 60% or greater. <P>COPYRIGHT: (C)2010,JPO&INPIT

Description

  The present invention relates to a method for purifying and producing vegetable oil.

  As a method for squeezing vegetable oil, a complete squeezing method, a hexane extraction method, or a combined squeezing-hexane extraction method has been mainly used. In recent years, the hexane extraction method has been reviewed for safety and environmental considerations, and many methods that do not use a solvent have been adopted. The obtained crude oil contains various impurities, although there are some due to the oil extraction method, and in order to use it for edible oil use, chemical use, etc., it was necessary to combine refining steps.

  There are roughly two methods for refining vegetable oil: chemical refining and physical refining. The former process is divided into degumming, alkaline deoxidation, decolorization, and deodorization, and the latter is divided into degumming, decolorization, and deodorization processes. The degumming process is a process for removing gum contained in crude oil, and is a process common to chemical and physical refining. Specifically, a method of adding an acid, a method of using an enzyme, a method of using a membrane, and the like have been developed (Non-Patent Document 1). Also, a technique for adding a surfactant as a degumming agent to fats and oils and removing impurities in the fats and oils (Patent Document 1), and a method of adding a mixture of two or more acids and surfactants as degumming agents (patents) Reference 2) has been reported. Examples 68 to 70 of Patent Document 3 describe a method of adding a solution containing 0.5% by weight of sodium lauryl sulfate after adding a citric acid solution to water-degummed soybean oil. Yes. In addition, a technique for degumming by adding egg yolk phospholipid (Patent Document 4), a technique for degumming with a large amount of water (300 wt% oil) using sodium lauryl sulfate and EDTA salt (Patent Document 5), A technique for degumming (wax removal) with sodium lauryl sulfate and phosphate has been reported (Patent Document 6).

US Pat. No. 2,525,702 International Publication No. 1995/000609 Pamphlet JP-A-51-112810 JP-A-2-255896 JP-A-9-501453 US Pat. No. 3,994,943

Oreoscience, Japan Oil Chemists' Society, March 1, 2006, Vol. 6, No. 3, pp. 3-21

  Known impurities in vegetable oils include phosphorus compounds mainly composed of phospholipids, sterol glycosides (sugar sterols), vitamin E, and the like. However, no simple means for purifying by selectively reducing or removing all or a specific substance has not been found. Although the method of Patent Document 1 can reduce the phosphorus compound that is a gum, it cannot reduce sterol glycosides (sugar sterols), which are other impurities.

  An object of the present invention is to provide a method for efficiently reducing / removing a phosphorus compound mainly composed of a phospholipid contained as an impurity in a vegetable oil and a sterol glycoside (sugar sterol) from the vegetable oil.

The present invention relates to a method for refining and producing vegetable oil comprising the following steps 1 to 3.
Step 1: One or more non-phosphorous surfactants selected from an anionic surfactant, a cationic surfactant, and an amphoteric surfactant or a non-phosphorous interface selected from vegetable oils containing a sterol glycoside and a phosphorus compound Step 2 to obtain a mixture by adding a solution containing an activator Step 2: In the mixture obtained in Step 1, the water content in the mixture is 0.1 to 80 wt.% Relative to the vegetable oil used in Step 1. % Of water to obtain a mixture containing aggregates Step 3: Separation of aggregates from the mixture obtained in Step 2 results in the removal rate of sterol glycosides and phosphorus compounds. The process of obtaining vegetable oil which is 60% or more respectively.

  In addition, the present invention provides a method for producing an ester compound in which an ester reaction is performed as Step 4 on the vegetable oil obtained by the above-described method of the present invention, and the ester compound obtained by the method of the present invention. Step 5 relates to a method for producing an alcohol compound that performs a hydrogenation reaction.

  ADVANTAGE OF THE INVENTION According to this invention, the method of reducing and removing the phosphorus compound and sterol glycoside (sugar sterol) which have as a main component the phospholipid contained as an impurity in vegetable oil from vegetable oil efficiently is provided. In addition, in the method of the present invention, vitamin E, which has an excellent antioxidant effect and is useful as a edible oil and as a chemical raw material, can be retained in vegetable oil.

  In the purification of vegetable oil containing a sterol glycoside and a phosphorus compound, the present invention adds a specific non-phosphorous surfactant or a solution containing the non-phosphorous surfactant as step 1 and step 2 as step 1. Water is added so as to be 0.1 to 80% by weight with respect to the used vegetable oil to carry out a treatment to produce aggregates, and in step 3, the aggregates containing impurities are separated. That is, an aggregate containing an insoluble component efficiently by adding a specific non-phosphorous surfactant or a solution containing the non-phosphorous surfactant in step 1 and adding a predetermined amount of water in step 2. After that, by performing centrifugation, filtration separation, etc. in step 3, the agglomerates containing insoluble components are reduced and removed, and the vegetable oil is purified and produced. Furthermore, this invention provides the manufacturing method of the ester compound and alcohol compound using the vegetable oil obtained by doing in this way.

<Step 1>
In Step 1, one or more non-phosphorous surfactants selected from anionic surfactants, cationic surfactants and amphoteric surfactants or non-phosphorous surfactants are added to vegetable oils containing sterol glycosides and phosphorus compounds. Add a solution containing a surfactant.

  The vegetable oil is not particularly limited, but includes palm oil, palm oil, palm kernel oil, palm kernel olein, palm kernel stearin, soybean oil, rapeseed oil, corn oil, sunflower oil, Jatropha oil, algal oil, and the like. It is done. Preferably, one or more vegetable oils selected from the group consisting of palm oil, palm oil, palm kernel oil, palm kernel olein, rapeseed oil, sunflower oil and soybean oil, more preferably palm oil, palm oil, palm kernel oil, One or more vegetable oils selected from the group consisting of rapeseed oil. Generally, these vegetable oils, especially vegetable oils obtained by the complete pressing method, contain about 1 to 500 ppm of sterol glycosides and about 1 to 1000 ppm of phosphorus compounds before purification.

  The non-phosphorous surfactant is preferably one or more non-phosphorous surfactants selected from anionic surfactants and amphoteric surfactants, and one or more non-phosphorous surfactants selected from amphoteric surfactants. An activator is more preferred.

  The anionic surfactant is not particularly limited, and examples thereof include alkyl sulfates, alkyl ether sulfates, alkyl ether carboxylates, and alkylbenzene sulfonates. These alkyl groups preferably have 8 to 18 carbon atoms, more preferably 10 to 16 carbon atoms, and particularly preferably 12 to 14 carbon atoms. In addition, the ether compound preferably has an average addition mole number of alkylene oxide of 2 to 10, and examples of the alkylene oxide include ethylene oxide and propylene oxide. An anionic surfactant selected from alkyl sulfates, alkyl ether sulfates and alkylbenzene sulfonates is preferred. More preferred is an anionic surfactant selected from alkyl sulfates and alkyl benzene sulfonates.

  The cationic surfactant is not particularly limited, but alkyl (preferably having 8 to 22 carbon atoms, more preferably 10 to 18 carbon atoms, particularly preferably 12 to 14 carbon atoms) trimethylammonium chloride, alkyl. (Preferably having 8 to 22 carbon atoms, more preferably 10 to 18 carbon atoms, particularly preferably 12 to 14 carbon atoms) trimethylammonium bromide, dialkyl (preferably having 8 to 18 carbon atoms, more preferably having 10 to 16 carbon atoms, Particularly preferred are C12-14) dimethylammonium chloride, alkyl (preferably C8-18, more preferably C10-16, and particularly preferably C12-14) benzyldimethylammonium chloride. More preferred is a cationic surfactant selected from alkyltrimethylammonium chloride and alkylbenzyldimethylammonium chloride.

  The amphoteric surfactant is not particularly limited, but sulfobetaines such as alkylamidopropylsulfobetaine, alkylsulfobetaine, alkylhydroxysulfobetaine, carbobetaines such as alkylamidopropylcarbobetaine, alkylcarbobetaine, alkyl An amine oxide etc. are mentioned. An amphoteric surfactant selected from carbobetaine and sulfobetaine is preferable. These alkyl groups preferably have 8 to 18 carbon atoms, more preferably 10 to 16 carbon atoms, and particularly preferably 12 to 14 carbon atoms.

  In step 1, the non-phosphorus surfactant or a solution containing the non-phosphorus surfactant is added in an amount of 0.01 to 10% by weight, more preferably 0.05 to 5% by weight, based on the vegetable oil as an effective component of the non-phosphorus surfactant. Furthermore, it is preferable to add 0.1 to 1 weight%. In addition, it is preferable not to use a phosphorus-type surfactant in the process 1 from a viewpoint of the reduction of a phosphorus compound and a sterol glycoside, and the removal effect. Therefore, in the surfactant used in Step 1, the proportion of the non-phosphorus surfactant is preferably 50 to 100% by weight, more preferably 90 to 100% by weight, and further preferably 100% by weight.

  The non-phosphorus surfactant can be added to the vegetable oil as it is or as a solution containing other components (hereinafter also referred to as a non-phosphorus surfactant solution or simply a solution). In the case of a solution, the content (effective content) of the non-phosphorous surfactant is preferably 5% by weight or more and less than 100% by weight. From the viewpoint of the amount of material in operation, it is more preferably 10% by weight or more, more preferably 15% by weight or more, more preferably 20% by weight or more, and more preferably 25% by weight or more. On the other hand, from the viewpoint of workability in operation, it is more preferably less than 100% by weight, more preferably 80% by weight or less, more preferably 65% by weight or less, more preferably 50% by weight or less. From the viewpoint of actual operability, it is 10 to 80% by weight, more preferably 20 to 65% by weight, and more preferably 25 to 50% by weight.

  Examples of components that can be contained in the non-phosphorous surfactant solution include water, methanol, ethanol, isopropanol, acetone, and hexane.

  Further, the form when the non-phosphorous surfactant is used as it is may be either liquid or solid. Moreover, dispersions (preferably aqueous dispersions) such as emulsions and suspensions of non-phosphorous surfactants can also be used. Further, a solid mixture containing a solid non-phosphorous surfactant and other solid components can also be used. In the case of a solid, a powder composition is preferable. Examples of components that the mixture may contain in the case of a solid include sodium chloride, water, and alcohol.

  From the viewpoint of workability, it is preferable to use a solution of a non-phosphorous surfactant, particularly an aqueous solution. When using a solution of a non-phosphorous surfactant, the whole amount to be finally added may be added at once, or may be added in divided portions. Moreover, you may add continuously and may add intermittently. The amount of water added with the addition of the aqueous surfactant solution is preferably 80% by weight or less, more preferably 10% by weight or less, and still more preferably 1% by weight or less based on the vegetable oil used.

  In step 1, it is preferable to add a non-phosphorous surfactant or non-phosphorous surfactant solution in a state where the vegetable oil is heated to 30 to 90 ° C. Further, it is preferable to add the non-phosphorous surfactant or the non-phosphorous surfactant solution in a state where the vegetable oil is stirred.

  In step 1, after adding the non-phosphorous surfactant or non-phosphorous surfactant solution to the vegetable oil, stirring is performed at 30 to 90 ° C, further 40 to 90 ° C, and further 50 to 90 ° C for 1 minute to 10 hours. It is preferable from the viewpoint of operability to perform the operation of step 2 after mixing. Here, the stirring and mixing time is preferably 3 minutes or more, more preferably 5 minutes or more, and preferably within 5 hours, more preferably within 1 hour, more preferably from the viewpoint of handling and operability. Is within 30 minutes.

  For the stirring and mixing in step 1, both batch type and continuous type can be used.

<Step 2>
In step 2, water is added to the mixture obtained in step 1 to obtain a mixture containing aggregates. In Step 2, water is added so that the content of water in the mixture obtained in Step 1 is 0.1 to 80% by weight with respect to the vegetable oil used in Step 1. Here, the lower limit is preferably 0.5% by weight or more, more preferably 1% by weight or more, further preferably 2% by weight or more, still more preferably 3% by weight or more, and particularly preferably 5% by weight or more. . On the other hand, the upper limit is preferably 75% by weight or less, more preferably 50% by weight or less, and still more preferably 20% by weight or less. From the viewpoint of workability in the actual process, in the process 2, the amount of water in the mixture obtained in the process 1 is 0.1 to 80% by weight with respect to the vegetable oil used in the process 1. Add water. Deionized water, tap water, or the like can be used as the water, and it may contain other components (such as a sterilizing component) in an amount that does not affect aggregation.

  The amount of water added in step 2 is preferably 0.1 to 80% by weight with respect to the vegetable oil used in step 1. Here, it is more preferably 2% by weight or more, more preferably 3% by weight or more, more preferably 5% by weight or more, and more preferably 50% by weight or less, more preferably 20% by weight or less.

  The temperature of the mixture obtained in step 1 when adding water is preferably 30 to 90 ° C, more preferably 50 to 90 ° C, and after adding water, 30 to 90 ° C, further 40 to 90 ° C, It is preferable to stir and mix at 50 to 90 ° C. for 5 minutes to 5 hours. Here, from the viewpoint of cohesiveness, the stirring and mixing time at the temperature is preferably 10 minutes or more, more preferably 20 minutes or more. Further, from the viewpoint of economy, the stirring and mixing time at the temperature is preferably 3 hours or less, more preferably 1 hour or less, and more preferably 30 minutes or less. Further, from the viewpoint of operability, it is preferable to stir and mix at this temperature for 5 to 30 minutes, and further for 10 to 30 minutes. The stirring conditions at that time are preferably a batch type or a continuous type. As for the addition of water, the whole amount to be finally added may be added at once, or may be added in divided portions. Moreover, you may add continuously and may add intermittently. For the stirring and mixing in step 2, the same means as in step 1 can be used.

  Further, when an aqueous solution or aqueous dispersion of a non-phosphorous surfactant is used in step 1, the amount of water (W1) added in step 1 by the aqueous solution or aqueous dispersion and the water added in step 2 In the total with the amount (W2), the ratio of W2 is preferably 50% by weight or more and less than 100% by weight, more preferably 70% by weight or more and less than 100% by weight.

  In the present invention, the non-phosphorus surfactant or the non-phosphorus surfactant solution in step 1 is made to vegetable oil (preferably 40 to 90 ° C., more preferably heated to 50 to 90 ° C.). As an effective component of the non-phosphorous surfactant, 0.01 to 10% by weight is added, and in step 2, water is added to 1 to 1000% by weight with respect to the vegetable oil, and then maintained at 30 to 90 ° C. for 5 minutes to 5 hours. Preferably, maintaining under stirring is preferable in order to obtain a vegetable oil in which the removal rate of sterol glycoside and phosphorus compound is 60% or more, respectively. The stirring conditions in step 2 are preferably batchwise or continuous.

<Step 3>
In step 3, vegetable oils with a sterol glycoside and phosphorus compound removal rate of 60% or more are obtained by separating the aggregates from the mixture obtained in step 2. Here, the removal rate of sterol glycoside is preferably 70% or more, more preferably 80% or more, more preferably 90% or more, and more preferably 95% or more. Further, the removal rate of the phosphorus compound is preferably 70% or more, more preferably 80% or more, more preferably 90% or more, and more preferably 95% or more.

  In addition, in this invention, the removal rate (%) of a sterol glycoside and a phosphorus compound is calculated | required as follows. Moreover, the content of the sterol glycoside and the phosphorus compound in the vegetable oil (crude oil and refined oil) is measured by the method of Examples described later.

Removal rate of sterol glycoside (%) = [1- (sterol glycoside content in vegetable oil after separation of aggregates) / (sterol glycoside content in vegetable oil (crude oil)]] × 100

Phosphorus compound removal rate (%) = [1- (phosphorus compound content in vegetable oil after separation of aggregates) / (phosphorus compound content in vegetable oil (crude oil)]] × 100

  Usually, the vegetable oil which passed through the process 1 and 2 has produced | generated the aggregate containing an insoluble component, and the sterol glycoside and the phosphorus compound are contained in this aggregate. In addition, although such aggregates are hardly soluble in vegetable oils, the specific non-phosphorous surfactant selected in the present invention is excellent in the ability to disperse such aggregates in water. Is assumed to be easier. Therefore, in Step 3, if the aggregate is removed using a method known as a solid-liquid or liquid-liquid separation means, the removal rate of sterol glycoside and phosphorus compound is 60% or more, respectively. Can be obtained.

  Specific separation methods include centrifugation, stationary separation, filtration, or a combination thereof. In the case of centrifugation, it can be carried out under conditions of 40 to 100 ° C., preferably 40 to 70 ° C. and 1,000 to 100,000 G, preferably 5,000 to 50,000 G.

  The vegetable oil which passed through the process 3 can be processed according to a normal refinement | purification method.

  Moreover, about the vegetable oil which passed through the said processes 1-3 and contains vitamin E, vitamin E can be hold | maintained a lot compared with a normal method (it is not lost). Here, as a retention rate of vitamin E, 80% or more is preferable, 90% or more is more preferable, and 95% or more is more preferable.

  In the present invention, the retention rate (%) of vitamin E is determined as follows. Moreover, the content of vitamin E in the vegetable oil (crude oil and refined oil) is measured by the method of Examples described later.

Retention rate of vitamin E (%) = [(content of vitamin E in vegetable oil after separation of aggregates) / (content of vitamin E in vegetable oil (crude oil)]] × 100

  Furthermore, in this invention, the manufacturing method of the ester compound which performs ester reaction is provided as process 4 with respect to the vegetable oil obtained by the method of the said invention. The ester reaction in step 4 can be performed by a known method. The reaction can be performed in either a continuous or batch mode, but a continuous reaction is advantageous when a large amount of ester is produced. As the catalyst, a homogeneous alkaline catalyst such as sodium hydroxide, potassium hydroxide or sodium alcoholate is generally used, but solid catalysts such as ion exchange resin, hydrous zirconium oxide, aluminum phosphate, sulfuric acid-supported zirconia, titanosilicate, etc. Can also be used. When using a homogeneous alkali catalyst, the reaction is generally carried out under the following conditions. The reaction temperature is 30 to 90 ° C., preferably 40 to 80 ° C., and the reaction pressure is in the range of normal pressure to 0.5 MPa, preferably normal pressure.

  Furthermore, in this invention, the manufacturing method of the alcohol compound which performs a hydrogenation reaction is provided as process 5 with respect to the ester compound obtained by the method of the said invention. Step 5 includes a method in which an ester compound such as a fatty acid ester is used as a raw material and a hydrogenation reaction is performed using a hydrogenation catalyst. As the hydrogenation catalyst, a commonly known copper-based or noble metal-based catalyst such as palladium or platinum is used. Examples of the copper-based catalyst include copper-chromium, copper-zinc, copper-iron-aluminum, and copper-silica. In the presence of any of the above catalysts, the hydrogenation reaction can be carried out by any commonly used reaction method such as a liquid phase suspension bed or a fixed bed method.

  When the reaction is carried out in a liquid phase suspension bed system, the catalyst amount is preferably 0.1 to 20% by weight based on the ester compound such as a fatty acid ester, but depending on the reaction temperature or reaction pressure, a practical reaction yield. Can be arbitrarily selected within the range in which is obtained. The reaction temperature is preferably 160 to 350 ° C, more preferably 200 to 280 ° C. The reaction pressure is preferably 0.1 to 35 MPa, more preferably 3 to 30 MPa.

  When the reaction is carried out continuously in a fixed bed system, the catalyst used is a cylinder, pellet, or sphere. The reaction temperature is preferably 130 to 300 ° C, more preferably 150 to 270 ° C, and the reaction pressure is preferably 0.1 to 30 MPa. LHSV is arbitrarily determined according to reaction conditions in consideration of productivity and reactivity.

  The amounts of phosphorus compound (ppm), sterol glycoside (ppm), and vitamin E (ppm) contained in the vegetable oil (crude oil) used in the following examples and comparative examples are shown in Table 1 below. In addition, the phosphorus compound content of vegetable oil (crude oil) and its refined oil was measured based on the standard oil analysis method 2.4.11-2003 (phosphorus) [edited by Japan Oil Chemists' Society, 2003 edition]. The content of sterol glycosides in vegetable oil (crude oil) and its refined oil is a method described in Lipids, 34 (11), 1231 (1999) (published by American Oil Chemists' Society). Measured with Further, the content of vitamin E was measured based on the standard oil analysis method 2.4.10-2003 (tocopherol) [edited by Japan Oil Chemists' Society, 2003 edition].

Example 1
A vertically long 500 cc separable flask was used as a reaction vessel. While stirring 200 g of coconut crude oil (stirring using a mechanical stirrer, 6-blade stainless steel blades with a diameter of 60 mm, rotating at 580 rpm), the temperature was raised to 60 ° C. and 30% (% by weight, hereinafter surface activity) The same as for the aqueous agent solution) 1.2 g of an aqueous solution of dodecylamidopropylcarbobetaine was added and stirred for 5 minutes at 60 ° C. Thereafter, 20 g of water was added and stirring was further continued for 30 minutes at 60 ° C. to obtain a mixture containing aggregates. The obtained mixture was centrifuged at 15,000 G for 10 minutes under the condition of 60 ° C. (HITACHI himac CR22F), and the aqueous phase containing aggregates was separated by decantation to obtain purified coconut oil. The phosphorus compound content and sterol glycoside content of the refined coconut oil were measured, and the removal rate was determined by comparison with that of coconut crude oil.

Comparative Example 1
In Example 1, the temperature rise of palm crude oil was 40 ° C., a mixture of 1.2 g of 30% aqueous dodecylamidopropylcarbobetaine and 20 g of water was added, and the mixture was stirred for 30 minutes. From the resulting mixture, gum water was separated in the same manner as in Example 1 to obtain purified coconut oil. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 2.

Comparative Example 2
In Comparative Example 1, refined coconut oil was obtained in the same manner except that the temperature of the coconut crude oil was raised to 60 ° C. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 2.

  As shown in Table 2, sterol glycosides cannot be removed sufficiently in Comparative Example 1 and Comparative Example 2, but in Example 1, a high removal rate is achieved for both sterol glycosides and phosphorus compounds. .

Examples 2 to 4 and Comparative Examples 3 to 5
In Example 1, instead of a 30% aqueous solution of dodecylamidopropylcarbobetaine as a surfactant, a 98% aqueous solution of sodium dodecyl sulfate (Example 2, Comparative Example 3), a 26% aqueous solution of sodium dodecylbenzenesulfonate (Example 3, Comparative) Example 4), except for using 50% aqueous solution of dodecylbenzyldimethylammonium chloride (Example 4, Comparative Example 5). In the same manner as in No. 1, purified palm oil was obtained. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 3.

  As shown in Table 3, sterol glycosides could not be removed sufficiently in Comparative Examples 3 to 5, but in Examples 2 to 4, high removal rates were achieved for both sterol glycosides and phosphorus compounds. .

Examples 5-7
A refined oil was obtained in the same manner as in Example 1 except that palm crude oil (Example 5), rapeseed crude oil (Example 6), or sunflower crude oil (Example 7) was used as the fat raw material. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. Vitamin E retention was also measured. The results are shown in Table 4.

  From the results of Table 4, the method of the present invention is an operation effective for removing impurities even for palm oil, rapeseed oil, and sunflower oil, and that vitamin E, which is a useful component, can be retained very efficiently. I understand.

Example 8
In Example 1, soybean crude oil was used as the fat and oil raw material, the surfactant addition amount was 0.3 wt% (effective amount) with respect to the oil, and the water addition amount was 20 wt% (40 g) with respect to the oil. A refined oil was obtained in the same manner except that. The sterol glycoside and phosphorus compound removal rate was determined in the same manner as in Example 1, and the vitamin E retention rate was determined in the same manner as in Example 5. The results are shown in Table 5.

  From the results of Table 5, it can be seen that the method of the present invention is an operation effective for removing impurities even for soybean oil, and vitamin E, which is a useful component, is retained extremely efficiently.

Example 9
While stirring 200 g of coconut crude oil, the temperature was raised to 40 ° C., and 1.2 g of 30% dodecylamidopropylcarbobetaine aqueous solution was added, and the mixture was stirred at 40 ° C. for 5 minutes. Thereafter, 20 g of water was added and stirring was further continued for 3 hours at 40 ° C. The obtained mixture was centrifuged at 15,000 G for 10 minutes, and gum water was separated by decantation to obtain purified coconut oil. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 6.

  From the results of Table 6, it can be seen that, in Step 2, a high sterol glycoside and phosphorus compound removal rate is exhibited by stirring at 40 ° C. for 3 hours.

Example 10
While stirring 200 g of coconut crude oil, the temperature was raised to 90 ° C., and 1.2 g of 30% dodecylamidopropylcarbobetaine aqueous solution was added, and the mixture was stirred at 90 ° C. for 5 minutes. Thereafter, 20 g of water was added and stirring was further continued for 1 hour at 90 ° C. The obtained mixture was centrifuged at 15,000 G for 10 minutes, and gum water was separated by decantation to obtain purified coconut oil. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 7.

  From the results in Table 7, it can be seen that, in Step 2, stirring at 90 ° C. for 1 hour shows a high removal rate of sterol glycosides and phosphorus compounds.

Examples 11-16
In Example 1, instead of 30% dodecylamidopropylcarbobetaine aqueous solution as a surfactant, 30% cocoamidopropylbetaine aqueous solution (Example 11), 26% dodecylcarbobetaine aqueous solution (Example 12), 26% stearylcarbo Betaine aqueous solution (Example 13), 40% 2-dodecyl-N-carboxymethyl-N-hydroxyethylimidazolinium betaine aqueous solution (Example 14), 30% aqueous dodecylhydroxysulfobetaine aqueous solution (Example 15), 30% Coco A refined coconut oil was obtained in the same manner as in Example 1 except that the aqueous amidopropylamine oxide solution (Example 16) was used. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The vitamin E retention was determined in the same manner as in Example 5. The results are shown in Tables 8 and 9.

  From the results of Tables 8 and 9, it can be seen that by using an amphoteric surfactant, a high removal rate of sterol glycosides and phosphorus compounds is exhibited. Moreover, it turns out that vitamin E which is a useful component is hold | maintained very efficiently.

Comparative Example 6
In Example 1, a purified coconut oil was obtained in the same manner as in Example 1 except that 99% dipalmitoyl phosphatidylcholine (Comparative Example 6) was used in place of the 30% dodecylamidopropylcarbobetaine aqueous solution as the surfactant. . The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 10.

  As shown in Table 10, in Comparative Example 6, the sterol glycoside cannot be removed sufficiently.

Comparative Example 7
In Example 1, refined coconut oil was obtained in the same manner as in Example 1 except that 99% dilauryl phosphate (Comparative Example 7) was used instead of the 30% dodecylamidopropylcarbobetaine aqueous solution as the surfactant. . The sterol glycoside removal rate was determined in the same manner as in Example 1. The results are shown in Table 11. Table 11 also shows the phosphorus compound content.

  As shown in Table 11, in Comparative Example 7, the sterol glycoside cannot be removed sufficiently. Moreover, since the dilauryl phosphate used as the surfactant remains in the refined oil, the phosphorus compound cannot be removed sufficiently.

Comparative Example 8
In Example 1, refined coconut oil was obtained in the same manner as in Example 1 except that the amount of water added was increased to 100% by weight. The sterol glycoside removal rate was determined in the same manner as in Example 1. The results are shown in Table 12. Table 12 also shows the phosphorus compound removal rate.

  As shown in Table 12, in Comparative Example 8 having a large amount of water, sterol glycosides cannot be sufficiently removed.

Example 17
In Example 1, refined coconut oil was obtained in the same manner as in Example 1 except that the amount of water added in Step 2 was changed to 0.2 g. The removal rate of sterol glycoside and phosphorus compound was determined in the same manner as in Example 1. The results are shown in Table 13.

  As shown in Table 13, in Example 17, a vegetable oil in which the removal rate of sterol glycoside and phosphorus compound is 60% or more can be obtained as in Example 1.

Claims (9)

A method for purifying and producing vegetable oil comprising the following steps 1 to 3.
Step 1: One or more non-phosphorous surfactants selected from an anionic surfactant, a cationic surfactant, and an amphoteric surfactant or a non-phosphorous interface selected from vegetable oils containing a sterol glycoside and a phosphorus compound Step 2 to obtain a mixture by adding a solution containing an activator Step 2: In the mixture obtained in Step 1, the water content in the mixture is 0.1 to 80 wt.% Relative to the vegetable oil used in Step 1. % Of water to obtain a mixture containing aggregates Step 3: Separation of aggregates from the mixture obtained in Step 2 results in the removal rate of sterol glycosides and phosphorus compounds. The process of obtaining vegetable oil which is 60% or more respectively.   The non-phosphorous surfactant is one or more non-phosphorous surfactants selected from anionic surfactants comprising alkyl sulfates, alkyl ether sulfates and alkylbenzene sulfonates, and amphoteric surfactants comprising carbobetaines and sulfobetaines. The method for purifying and producing vegetable oil according to claim 1, which is an agent.   The vegetable oil is one or more vegetable oils selected from the group consisting of palm oil, palm kernel oil, palm kernel olein, palm kernel stearin, palm oil, rapeseed oil, sunflower oil, soybean oil, Jatropha oil and algal oil. Item 3. A method for purifying and producing vegetable oil according to Item 1 or 2.   In step 1, after adding the non-phosphorus surfactant or the solution containing the surfactant to the vegetable oil, the mixture is stirred and mixed at 30 to 90 ° C for 1 minute to 10 hours, and then the operation of step 2 is performed. Item 4. The method for purifying and producing vegetable oil according to any one of Items 1 to 3.   The solution containing the non-phosphorus surfactant in step 1 is a solution containing 5 wt% or more and less than 100 wt% of the non-phosphorus surfactant as an effective component. The refinement | purification and manufacturing method of vegetable oil of description.   The solution containing the non-phosphorus surfactant in step 1 is a solution containing 20 wt% or more and less than 100 wt% of the non-phosphorus surfactant as an effective component. The refinement | purification and manufacturing method of vegetable oil of description.   In step 1, the non-phosphorous surfactant or a solution containing the non-phosphorous surfactant is added in an amount of 0.01 to 10% by weight to the vegetable oil as an effective component of the non-phosphorous surfactant. The method for purifying and producing vegetable oil according to any one of the above.   The manufacturing method of the ester compound which performs ester reaction as process 4 with respect to the vegetable oil obtained by the method of any one of Claims 1-7.   The manufacturing method of the alcohol compound which performs a hydrogenation reaction as process 5 with respect to the ester compound obtained by the method of Claim 8.