JPS5876500A - Purification of oil and fat and product thereof - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for total purification of crude vegetable oils and fats. Among other things, the present invention relates to a method for purifying impure crude fats and oils in order to yield a hydrologically additive-free product with good oxidation stability, flavor stability and low temperature test stability.

In the past, edible oils and fats obtained from animals were refined using physical refining methods. However, vegetable oils and fats could not be sufficiently purified by such methods. The wide variety of impurities contained in vegetable fats and oils result in undesirable properties in the final product, such as darkening of the color and alteration of the fishy flavor.

At present, one of the most common methods for refining vegetable oils and fats is to treat the crude oils and fats with an alkali. This alkaline purification removes free fatty acids and other acidic substances,
Removes some of the phosphorous substance, proteinaceous substances, pigments, and trace amounts of metals.

Until recently, most oils and fats could only be satisfactorily deodorized by alkali purification. However, alkaline refining is suitable as a preparatory treatment for further processing of various oils, such as bleaching and deodorization.
1 It also has some serious drawbacks.

The alkalinity a generally also suffers from a large loss of neutral oil components of crude oils, thereby reducing the yield of refined oil products. In addition, removal of free fatty acids by alkaline refining results in the production of soap raw material which must be further processed for recovery as its fatty acid t-byproduct.

Additionally, alkaline refining generally produces large amounts of wastewater, which often causes significant wastewater pollution. Additionally, alkaline-refined oils are often treated with various stabilizers, typically Ka antioxidants and citric acid, to ensure that the refined oil maintains acceptable flavor characteristics and prevents harmful oxidation during storage. etc. is required.

Alkaline refining also includes a dewaxing step, which increases the price of the refined oil. This additional step is a process for removing not only compounds classified as waxes in a strict chemical sense, but also compounds that are insoluble at low temperatures, so-called waxes. If a processing step is employed to cool the fat and remove the solids formed, the final product fat will not exhibit acceptable low temperature test stability, i.e. such fat will not be exposed to 0°C for 24 hours. Good transparency will no longer be maintained in the container stored in the container. Various methods for physically refining vegetable oils and fats have been proposed in recent decades. Some of these methods have already been successful for certain crude oils and fats containing limited amounts of various types of impurities; for example, U.S. Pat.
The invention of No. 845 relates to a method for bleaching animal and vegetable fats or oils, and the method consists of adding bleaching clay and sulfuric acid. In this method, the bleaching clay is added at least simultaneously with or before the added sulfuric acid, so that the oils and fats to be treated are exposed to the acid only in the presence of the bleaching clay. This is K.

The mixture is stirred and the supernatant oil layer is drawn off and passed through a layer of diatomaceous earth.

U.S. Patent No. 1964 to Mr. Freiberg,
The invention of No. 875 relates to an alkaline refining process, and this publication discloses one method for removing impurities from fats and oils, in which the fats and oils are mixed with a small amount of concentrated phosphorous. This mixture is then slowly heated to about 70°C,
Stir and add a small amount of cellulose. When the action of the added phosphoric acid and cellulose is complete, the fat and oil are separated and treated with P.

U.S. Patent No. 1,974 to Mr. ApplJtOn
The invention of No. 790 relates to a method for completely refining inedible vegetable oils and increasing their thermal stability for use in paints. In this method, fats and oils are purified by thoroughly mixing them with a sufficient amount of sulfuric acid to react with impurities in the fats and oils. Such impurities precipitate out and precipitate out of the oil in the form of sludge. This refined fat is then separated from the sludge.

U.S. Patent No. 2.44L awarded to Mr. 8ullivan
Although No. 925 is not per se concerned with physical refining methods, it does note that adsorbent materials activated with silica, such as activated clay, can be used to remove residual color from alkali-treated fats and oils. Disclosed.

U.S. Patent No. 2 to Mr. Ohristenson.
The invention of No. 51Q, No. 379 relates to a method for removing lecithin, other lipids, and coloring substances. After treating the fat with alkali, the fat is further treated with an equivalent amount of strong acid to remove the salt formed by the alkali and the added acid. For neutralization of fats and oils, phosphoric acid and other strong acids are used (see lines 24.35-42). This document also discloses the use of acid-activated bleaching clays (see lines 24.35-42). (See column 4, lines 10-15).

U.S. Patent No. 2,587 to Mr. Bayan
, No. 254 relates to a method for recycling contaminated waste palm oil used in steel manufacturing. According to this method, waste palm oil is treated using phosphoric acid, sulfuric acid, or hydrochloric acid of 1 to 5 parts by weight in water in an amount of at least 50 parts by weight of the oil at a temperature of 0 to 100°C. be done. 'The mixture is separated into layers and the oil layer is separated from the aqueous layer and bleached.

U.S. Patent No. 2,903,4 issued to Gros @ et al.
The invention of No. 34 does not relate to the purification of oils and fats, but relates to a method for producing activated bleaching clay.

Montmorillonite clay is treated with an aqueous solution of a total fluorine compound and with hydrochloric acid, phosphoric acid, or sulfuric acid.

U.S. Patent No. 2.9 issued to Mink 1son et al.
No. 8L697 discloses a method for preparing acid activated deodorizing clay. Acid activated subbentonite clay is treated with hydrogen chloride in an aqueous solution and then washed with water until substantially free of chloride ions. This aqueous clay is then treated with phosphoric acid or phosphoric acid at a temperature of about 50° C. or less to remove residual chlorine ions. Remove excess acid from this clay
The clay is then flash dried at a temperature below 100°C.

U.S. Patent No. 42 awarded to Mr. Van Akkeren
No. 84.215 is a triglyceride commonly used to suppress decomposition during heating and prevent foaming.

Discloses a method for treating fats and oils. About 0 for fats and oils
．． 05 to S, SS concentrated phosphoric acid tube is added and the fat is slowly heated to a temperature of about 100°C and stirred gently to prevent the formation of free acid in the fat. Bleaching clay is added to the oil once the temperature of the oil has reached approximately 100°C, and the mixture is then heated to approximately 15°C.
- Heat to about 120°C for 50 minutes. The oil is first cooled, filtered to remove clay and phosphoric acids, and then heated to about 220-225 DEG C. under reduced pressure. This reference teaches that prior to final heat treatment, using bleaching clay to remove all phosphoric acid is a mold cost. Phosphorus:
Ratios of clay up to 1:10 can be calculated from the examples.

U.S. Pat. Discloses a method for refining oil by making.

Particulate solids, such as acid white, earth, activated clay, or activated carbon, are then added to adsorb the refining agent and separate the fats and oils from the solids. Phosphoric acid is listed among the refining agents.

US patent number awarded to Mr. Telan! 1,590,0
No. 59 discloses a method for refining bulk and animal fats and oils containing fatty acids or other impurities.

First, the crude fat or gummy fat is washed with about 1 to 5iii% water, and the aqueous phase is separated from the resulting mixture. This washed oil is then treated with an organic acid such as formic, acetic, oxalic, lactic, citric, tartaric or succinic acid or anhydrides of these acids, and also mixtures of these acids. s g@% L' Process using less electricity. Moisture level of this oil t14
11111) and this oil 1! ! Cool white with white clay. Following this, the bleached oil is steam-evaporated under vacuum to remove all fatty acids. It has also been suggested to use mineral acids in place of organic acids.

U.S. Patent No. 4.115 awarded to Watana M Daigo
, 752 and British Patent No. 1.559.186 disclose a method for refining oils of the palm oil type. Crude palm-type oil, which is substantially free of phospholipids and in which all carotenoid compounds are in a substantially heat-sensitive state, is first treated with 0.01 to 2.0 parts by weight of phosphoric acid. Add. After mixing, activated clay is added and its aA degree is increased and maintained at about 100° C. for about 5 to 30 minutes. The clay is then separated from the oil, and the oil is purified and deodorized by steam distillation using superheated steam at a temperature of 200°-270°C.

The calculated ratio of phosphoric acid: bleaching clay is approximately 1:0.1 to 1.
= 60't.

U.S. Patent No. 489-04 to TIL710r
No. 2 relates to a method for refining crude vegetable oils and other fatty substances. Crude fatty substances under vacuum,
or heated in the presence of phosphoric acid and activated clay in an inert atmosphere to a temperature of about 325° to 50,016°. The product obtained is then treated with P.

One of the objects of the present invention is to provide a method for refining crude vegetable oils.

Another object of the present invention is to provide a method for purifying crude vegetable oils containing various impurities such as phospholipids, waxes, and trace metals.

Yet another object of the present invention is to provide a process for the purification of crude vegetable oils in which economically valuable by-products can be more easily recovered.

Another object of the present invention is to provide refined oil and fat products with increased stability of flavor properties.

Yet another object of the present invention is to provide refined oil and fat products with enhanced stability against oxidation.

Yet another object of the present invention is to provide a refined oil and fat product that has satisfactory low temperature test stability without the need for a separate cooling treatment step. These objects and features of the present invention,
and various advantages will become apparent in the detailed description of its preferred embodiments given below.

According to the present invention, in refining crude vegetable oil tubes to provide a product with good oxidation stability, flavor stability and low temperature test stability, the following process steps are carried out, namely (a) crude oil and fat. (I) By combining such crude oils and fats with a small amount of water to form a mixture, stirring this mixture, and (It) separating it from the oils and fats and water to precipitate impurities. (b) Gummy/metal removal of the gummy fat obtained in the above process step (a)-1) is carried out by applying (11) a small amount of a suitable known gum remover to the above fat and oil. (1) stir this mixture; () combine a small amount of water with this mixture; (&) stir the resulting mixture; and (7) remove any remaining impurities from the fat or oil. (1)
- At least 2/100% (ν
Combine such phosphoric acids in the form of an aqueous solution such that a mixture containing phosphoric acid with a concentration of 0.02 or more) is formed; maintained at a temperature of The whitening agents are combined in such proportions as to allow shallow levels of up to (V) bring the temperature suitable for the action of the bleaching agent and maintain this temperature while stirring the mixture throughout; (V)
and (4) filtering the bleached oil and fat obtained in process steps (c)-(■) above. Steam purification and deodorization of oils and fats.

A method for refining the above oil and fat is provided, including each process step.

According to another embodiment of the present invention, in refining crude vegetable fat tubes to provide a product with good oxidation stability, flavor stability, and low temperature test stability, the following steps are carried out: Steps (a) Gummy removal from the crude fats and oils are carried out by combining such crude oils and fats with a small amount of water to form a mixture, (1) stirring this mixture, and (It) separating it from the fat pipe water. (b) Bleaching the fat obtained in the above process step (i) (1) by adding at least 2/10 of 1 weight to the fat and oil.
0 (i.e. 0.02q11 or more) of phosphoric acid is combined in the form of an aqueous solution such that a mixture containing 0 (i.e. 0.02q11 or more) phosphoric acid is formed; The phosphorus content in the final product derived from the phosphoric acid added in step 1-(!11) is maintained at a temperature of Combine the bleaching agents in such proportions as to permit a residual level of S ppm '! and maintain this temperature while stirring the mixture; (V) bring the temperature of the mixture in the process steps of m (cooled in niO, and cVi) by filtering the bleached fat, and then (c) the bleached fat obtained in the process steps of The method for refining fats and oils is provided, which includes the steps of steam purification and deodorization.

According to yet another embodiment of the present invention, in refining crude vegetable oil to provide a product with good oxidation stability, flavor stability, and low temperature test stability, the following Each process step, i.e. ←) Removal of gummy matter/metal content from crude oil and fat (1)
combining the above fat and oil with a small amount of a suitable known degumming agent to form a mixture; (1) stirring the mixture; (optionally combining the mixture with a small amount of water); Bleaching of the fats and oils obtained in step (A)-(Vl-) above.

(1) At least 2/10 of 1 weight of the above fats and oils
0 (i.e., 0.021 or more) of phosphoric acid is formed in the form of an aqueous solution, (1) this mixture is thoroughly stirred with a suitable solution to allow the entire reaction to take place; ([1 1 mouthful 1- (ml) of the processed mixture in the process step,
5 in the final product of phosphorus content derived from the phosphoric acid added in (b)-(11) above 1) P! Combine the bleaching agents in such proportions as to permit a residual level of up to Bring the mixture to a temperature similar to that of the bleaching agent and maintain this temperature while stirring the mixture 1r.

It is cooled to a temperature K such that the vacuum can be released, and (■ is carried out by filtration of all the bleached fats and oils, and then (/1) There is provided a method for refining the above-mentioned fats and oils, which includes the steps of steam purifying and deodorizing the fats and oils.

According to yet another embodiment of the present invention, in preparing 11nI of crude oil and fat to provide a product with good oxidation stability, flavor stability, and low temperature test stability, the following The process steps, namely (a) bleaching of the crude oil and fat, are carried out in such a manner that a mixture containing at least 2/100 parts of phosphoric acid (i.e., not less than 0.02 parts) of phosphoric acid is formed in the above oil and fat. of phosphoric acid in the form of an aqueous solution, (11) this mixture being maintained at a suitable temperature to permit reaction while stirring vigorously; Add all bleaching agent combinations to the above mixture in such proportions as to permit a residual level of 5 ppm i in the final product of phosphorus derived from the phosphoric acid added in step 11. H> - The temperature of the mixture obtained in process step (1) is raised under vacuum to a temperature suitable for the action of the bleach selected above, and this temperature is increased while stirring the mixture. Maintaining the temperature of the mixture in the process step (C) above, cooling it to a temperature such that the vacuum can be released, and (VD) by filtering the bleached fat, Next, there is provided a method for refining fats and oils, which includes the steps of (b) steam purifying and deodorizing the bleached fats and oils obtained in the steps (i) to (vO) above.

The present invention clearly demonstrates that an edible oil with good flavor stability, oxidation resistance stability and low temperature test stability can be obtained by a physical refining method. The present invention is based on *lk+S products (residuals derived from the phosphoric acid used in the process according to the invention, 511% a)
This provides an oil having a content level of 1:1m or less.

Of course, the applicant of this patent does not wish to be bound to any one particular mechanism, but at the present stage phosphoric acid, which is added as an auxiliary agent in the refining process, is used to control trace components in the oil, such as chlorophyll, phospholipids, etc. and peroxidant metals, etc., during their treatment, and in the absence of phosphoric acid, the bleaching clay would have some difficult-to-explain effect on oils and fats. It is thought to prevent noise.

After this bleaching process, the phosphorus content has no further advantageous effect, and its removal after the action of the bleaching clay does not alter the advantageous properties of the fats and oils according to the invention. I believe it is tk%A. However, the residual levels of phosphorus up to sp ppm thus obtained are substantially lower than permissible levels, and since they are often used as additives in alkaline-refined fats and oils, this refining processing aid cannot be completely removed. It is believed that removal is unnecessary.

Residual levels of phosphorus up to 5 ppm in finished product fats and oils cannot be detected as phosphoric acid by conventional acidity measurements, and phosphorus content cannot be detected using the proven test method of 100B Official Method 40112-55. below the detection level.

Phosphate removal present in the form of phospholipids during bleaching does not result in fats and oils having superior properties according to the invention. It is believed that such phosphorus compounds do not have the ability to bind heavy metals such as iron or steel which would promote oxidation.

In order to obtain a product oil with such excellent properties, the processing process is such that essentially all the gold phosphate is removed without allowing the oil to be exposed to the action of bleach. Various parameters for such controlled removal of phosphoric acid, which must be carefully controlled, have been experimentally established. Treating the fat with excess bleach will remove all of the phosphoric acid. This is believed to have the same effect as treating the oil with bleach alone, which will improve the oxidative stability of the oil.

At residual phosphorus levels as high as s ppm, acidity becomes somewhat detectable, and refined fats and oils with phosphorus levels this high have satisfactory initial properties. However, these oils and fats possess these excellent properties! shall not be maintained.

In the present invention, unrefined vegetable oil is first pretreated to remove various impurities, and then purified with steam in step 2, which results in good oxidation stability, flavor stability, and cold test stability. It has been shown that product fats and oils can be obtained.

Vegetable oils and fats are known to contain many different types of impurities, which must be removed prior to steam purification; crude oils and fats may contain some or all of the following impurities: . These include free fatty acids, phospholipids that can be used as water, phospholipids that cannot be used as water, low-temperature insoluble portions (commonly referred to as 1 wax 1), trace metals, nodding agents, proteinaceous substances, and mucous substances. , mycotoxins.

Pesticides and oxidizing precursors. The process according to the invention can be applied to all commercially available oils, with the exception of cottonseed oil, which contains a dark red pigment commonly referred to as "gotssypol", which is believed to be able to be removed only by treatment with alkali. For example, it can be applied to corn oil, soybean oil, peanut oil, sunflower oil, safflower oil, rapeseed oil, rice sugar oil, coconut oil, palm oil, palm kernel oil, Babatus oil, and the like. These commercially known various oils and fats contain at least some of the various impurities listed above. Some oils, such as soybean oil and rapeseed oil, generally contain relatively high concentrations of hydratable and non-hydratable phospholipids, while other impurities, such as low-temperature insoluble The concentration of wax, etc. is at a level that does not present a removal problem.

While other fats and oils, such as corn oil and sunflower oil, contain relatively high levels of waxes and trace metals, phospholipids usually do not contain enough K to exhibit a high removal rate.

In addition, -q other oils and fats, such as palm oil, palm kernel oil, or coconut oil, can be purified by various physical purification methods that do not exhibit concentrations of impurities that require removal prior to bleaching and steam refining. It has been applied to such oils with some success. However, the present invention provides a process for refining such oils to obtain a variety of advantageous properties that have hitherto not been reliably achievable.

Most of the impurities listed above cannot become useful by-products, and no attempt is generally made to recover them.

However, free fatty acids and phospholipids are useful, and it is not unusual to attempt to recover them. Alkaline Purification Methods Therefore, only the removed free fatty acids can be recovered from the soap raw material formed, and they are generally of low quality. In the present invention, the removed phospholipids are Acidic oils obtained from soap raw materials which are of good quality and can be used as animal feed etc. or they can be further processed to recover commercial quality lentin. Higher quality free fatty acids can be obtained directly in a much purer form from their steam distillation.

It should be pointed out that the method described here is effective for removing mycotoxins, such as aflatoxin, from crude oils and fats. However, if such toxins are present, a product may contain these gold impurities.

Assuming that a certain crude oil contains a high concentration of low-temperature insoluble matter (wax), trace metals, and hydratable and non-hydratable phospholipids, this is the first treatment step. It is difficult to remove gum by using crude oil and Sat water.

Add a small amount of water, typically 1 to 5 parts by weight, and stir into the oil. Your water availability of this water must be sufficient to remove a significant amount of the compound.
The fats and oils are then separated by several practical methods, usually centrifugation or sedimentation.

This step can be carried out at any suitable temperature.
, and often the room temperature remains.

However, a lower temperature is effective for K to very effectively remove compounds commonly called ``waxes'' that do not dissolve in the oil at low temperatures.Therefore, such ``waxes'' exist. If so, it may be advantageous to terminate the process at a slightly lower temperature K, and temperatures in the range from about 5°C to about 20°C are most suitable.

Water-insoluble phospholipids and trace metals, such as iron, copper, calcium,! Another additional pre-treatment is required to remove magnesium etc. A small amount, typically less than 4 parts by weight of a suitable degumming agent and water are added to the fat and oil and stirred. The degumming agent can be selected from a number of known in the art, such as organic acids or inorganic acids or their anhydrides. Various emulsifiers and surfactants are also known to be important for this purpose. Agents currently known to be preferred are maleic acid, fumaric acid, citric acid, and phosphoric acid. Next, remove the gum.
'The fats and oils that have been treated for metal removal are separated from the heavy phase containing residual phospholipids and residual particulate metals.

The oil, which has been pretreated for bleaching by the process steps described above or by any other method known in the art, is then combined with a small amount of phosphoric acid in an aqueous solution. Preferably, a concentrated solution is used to reduce the need for subsequent removal with water.
The temperature must be sufficient to form a mixture containing phosphoric acid (above). Although it is possible to use higher amounts, phosphoric acid concentrations greater than about 0.2 weight range create problems with its removal, and the above concentration levels therefore represent an upper limit as a practical matter. The preferred range is about 5 in 1 weight range.
/100 (phosphoric acid with a weight range of 0.05 to 0.1 weight).

This mixture of fat and phosphoric acid is then stirred, advantageously with a slight increase in temperature.

about! Temperatures between 5° C. and 40° C. are generally advantageously used, provided that at higher temperatures, usually above 40° C., a vacuum may be applied to prevent harmful oxidative effects on oil deterioration. is considered necessary.

At this stage, a suitable amount of bleach, such as activated bleaching clay or acid clay, is added to remove most, but not all, of the previously added phosphoric acid. The bleaching agent t must be calculated to yield a final product fat with a level of up to 5 ppm residual phosphorus derived from the phosphoric acids mentioned above. A preferred bleaching agent is an activated bleaching clay which is commercially available under the trade name Filtrol 105™ sold by 111 Tro10 Corporation and which is described in some of the examples below. It is advantageously used in If no vacuum has been previously applied, the system should be brought to t-pressure prior to heating and stirring the mixture to a temperature suitable for the action of the bleaching agent used. Following the action of the bleach, the bleached fat must be filtered and the vacuum must not be removed until the oil has cooled sufficiently to prevent oxidation of the oil. Alternatively, the oil could be blanketed with an inert gas, such as nitrogen or carbon dioxide.

The thus bleached fats and oils can then be subjected to a steam refining/deodorizing step (by methods well known in the art) to complete the refining process.

The invention 1i is described in more detail below in illustrative examples.

Example 1 In the UK, application number A21 was filed on April 18, 1980.
Z, filed as No. 9ot and filed as UK Patent Application No. 7! on October 28, 1981. High quality corn oil was extracted from corn germ by the method described in the newsletter published as , No. 074183. This same technical disclosure was recently issued as US Pat. No. 4,54L715 claiming priority from this British patent application. The corn oil thus obtained was uncharacteristically free of phospholipids and "waxes" and was purified by the method according to the invention and, for comparison, by a conventional alkaline processing method, respectively. Some physical arrangement (chemical properties) of this crude oil and fat are listed in Table 1.

41q of this crude corn oil kept under vacuum at 40°C and an absolute pressure of 2 columns of mercury (jmHy).
The amount of i is 85% by weight of phosphoric acid in a highly concentrated aqueous solution - 4/
100 (i.e., 0.04 weight width) and stirred vigorously for 15 minutes.

Next, an amount of bleaching clay, commercially available from Filtrol Corporation under the trade name FILTROL 105 (registered trademark), in an amount of 1 oz per weight of oil and FILTROL® (trade name) At the bottom, Toh
2/2/1 inch of P additive available from ns-Manville Corporation based on the weight of fats and oils.
10 volumes were added to the vacuumed system described above. This system 1-
Heating to 120°C and vigorous stirring continued for an additional 20 minutes after which time the mixture was cooled to 80°C and the vacuum was broken using nitrogen gas.

The clarified oil was poured into a Buchner funnel and two portions of 2.5 kg each were weighed out.

One of the two parts was named Sample A and was blown to an absolute pressure of 0.21131 using blown water vapor containing 2% gold.
A steam bath/de-vapor treatment was performed at 240° C. for 90 minutes under H9 vacuum.

The other part was named sample B, in which K was added in the form of a 20% aqueous solution of citric acid, which is known to be a useful additive in alkaline refined fats and oils.
After obtaining the raw material for deodorizing treatment containing 00pp of citric acid, this sample was subjected to steam purification/under the same conditions as the above sample.
It was subjected to deodorization treatment. Some physical and chemical properties of these samples M and B are shown together in Table 1.

Comparative sample 1 using a conventional alkali purification method: Comparative sample 1 was prepared as follows. 401) of the same crude corn oil kept at 6.1 #? The oil was treated with 2.8 m of 1611Be' aqueous caustic soda and stirred vigorously for 15 minutes. The oil was then heated to 65° C. and stirred for an additional 15 minutes. Following this, use this oil for 1 hour! ri 9#(
? The acceleration constant of gravity (9,81 m/Hr) at the rate of
The precipitated soaps were separated by centrifugation at a centrifugal force of 1435 times that of aea, yi). In this example and in the following examples, centrifugation was carried out under special conditions (unless otherwise stated, all were carried out under these conditions). The oil, which had been thoroughly mixed, stirred, centrifuged each time and washed with K, was then dried for 20 minutes at a temperature of 100 DEG C. under a vacuum of 2 w.times.III f absolute pressure.

The color values were similarly measured at the time of each chromaticity measurement according to ψ8 Official Method 0 (1B-53). This data is also listed in Table 2.

The flavor stability test was conducted as follows.

That is, the samples were stored at 35°C in the dark with 10 air spaces above, and the flavor was determined after 2 months, after 5 months, and after 12 months (by a trained panel test). Each sample was scored according to a scale of scent intensity from 1 to 9t, with scale lf1 indicating complete absence of scent, and scale 9 indicating extremely strong scent. The results of these tests are listed in Table 3.

The panel test value determined by Sai was 99%, and the strength of the incense was considerably excessive.

Example 2 Significant amounts of impurities such as free fatty acids, phospholipids, waxes, etc.
Crude corn oil containing trace metals, proteinaceous substances, etc. was prepared by conventional manufacturing methods. In this process, crude oil, typically dried corn germ having a fat content of 45% to 45% by weight and a moisture content of 1.5 to 2,096%, is subjected to mechanical pressure in a screw press. Oil was extracted by exposure. The physical and chemical properties of this crude oil are listed in Table 4.

13.14 of this crude corn oil was mixed with 3.0 lbs. of distilled water and heated to 60"0!F. The oil was held at this temperature fK and stirred vigorously for 15 minutes.

The precipitated gum was separated by centrifugation.

The gummy oil obtained in this way 1851G
It was treated with 0.2% by weight phosphoric acid in the form of a concentrated aqueous solution. This oil was stirred vigorously for 15 minutes at 40°C, then 3% by weight distilled water was added, the temperature was raised to 60°C, and the oil was stirred for 15 minutes. metal complexes and t were removed. The first of each 5.2# portion of the degummed and demetallized oil was treated with 0.1 wt. of phosphoric acid in the form of an 85 mm thick aqueous solution.

This oil was then heated at −40° C. under a vacuum of 2 ml of absolute pressure for 15 minutes. Co q4 (bleaching clay) and a,6 width C filter aid) were added respectively.

This mixture was heated to 120°C and stirred for 20 minutes. The oil was cooled to 90°C, quenched with nitrogen gas in the vacuum tube, and the oil was passed through a Puchner filter.

2. Both from bleached oil obtained as kernels. sk
An amount of sample X and sample v in g were weighed.

As in Example 1, citric acid was added to the sample v in the form of an aqueous solution with a concentration of
It was made to yield ooppm of citric acid. Both samples were then subjected to a steam purification/deodorization treatment for 90 minutes at 240 DEG C. under a vacuum of 0.2 Hp absolute using a 2.0 liter steam injection. The physical and chemical properties for these samples are listed in Table 4.

6 of the oil that has undergone this gum removal and trace metal removal treatment.
．． A second portion consisting of 21 °C g was reacted with 5.4 g of a 16 °Bθ' caustic soda solution and stirred vigorously for 15 minutes at 40 °C. The oil was then heated to 65°C and heated for 15 minutes. The soap stock formed was separated from this oil by centrifugation. Next, add 10 parts by weight of hot distilled water to this oil and stir it 2 times [repeat]
The oil, washed each time by centrifugation, was then dried for 30 minutes at a temperature of 100 DEG C. under a vacuum of 2 mH1 absolute pressure.

This oil was bleached by addition of 2% by weight of the bleaching clay used in Example 1 above and 0.4% of transient aid, respectively. The mixture was heated to 120°C under a vacuum of 2 mup absolute and stirred for 20 minutes.The mixture was then cooled to 90°C, the vacuum was broken with nitrogen gas, and the oil was filtered through a Puchner suction filter. - It was filtered using. Each sample G is 2.5 #l and 2.
, sample Hf (weighed) was taken from the oil thus obtained.
Citric acid was added to the sample HK in the form of a 20% aqueous solution as in Example 1, thereby resulting in a citric acid concentration of 100% P% in the raw material for deodorization. Deodorization treatment was carried out at 240° C. for 90 minutes using 2 volumes of blown steam under a vacuum of 0.2 mH absolute pressure. Table 4 summarizes the physical and chemical properties of these samples.

Table 4 Sample F! 00 units 20 6 1.0 1.9 0.1
0.070 sample F 01025 6 1.0
2.5 0.1 0.096 Sample Ck O,01
050,51,60,10,098 sample HD, 010
5 0.5 1.0 0.0 0.091 Example 1
Each sample obtained above was subjected to a color conversion test and a flavor stability test according to the method used in .

The obtained data are summarized in Table ttlcS and Table 6.

□ The Australian panel judgment value in Table 6 had a 99% accuracy, indicating that the intensity of fragrance was considerably excessive.

Example 5 22 of pressed crude corn oil made by normal manufacturing method
1 15 equivalent to 5% at 0 weight placed in a stainless steel container equipped with a propeller stirrer of 60#t2 crystal
# of water is added to this oil and the mixture is brought to ambient temperature [1
(approximately 27° C.) and stirred at 250 rpm for 30 minutes.

The precipitated gum was separated in a Westfaria® centrifuge operating at a rotational speed of 71,100 rpm at an oil flow rate of 4.5 jkp/min.

The resulting degummed oil was degassed and dried under vacuum at 80 u Hf absolute for 70 minutes at 40 tl with stirring.

For this oil, 2.06 kg of food additive grade phosphoric acid, equivalent to over 11 weight in the form of an 8591 concentration aqueous solution? In addition,
The mixture was then stirred for an additional 50 minutes under vacuum. A 2,507 liter portion of this oil was pumped into a slurry tank and mixed with 62 Jcg of bleaching clay (Filtroll 105 as listed in Example 1 above), which is equivalent to 3 parts of the total baking soda in the oil. ) and 0.6t for total baking soda in oil
12.5 kg of temporary auxiliary material equivalent to 4 [JhOn8Manvi under the trade name of Bia0 Supercell
'lle C! (commercially available from J.P. Corporation). The mixture in the slurry tank was stirred vigorously for 5 minutes, then poured into the slurry tank, which was still under vacuum.
I returned it to the container. This mixture was heated to 112 G°C and at a rotation speed of 100 rpm Table 9 First 4.0 4.1 Second 5.7 3.25 months
4.5 5.18 months S, 4
5.4 Example 4 A typical sample of crude soybean oil was purified by a method according to the invention and for comparison by a conventional alkaline refining process.

Some physical and chemical properties of this oil were determined at each stage of both of these refining processes and are listed in Table 10.

14# of this crude soybean oil was heated to 40° C. in a glass container, then 3.0 weight percent distilled water was added and the oil was vigorously stirred for 20 minutes. Raise the temperature to 60°C and stir slowly) for a further 20°C.
The oil was then centrifuged for 1 minute to separate the hydrated phospholipids.

The oil thus obtained in the form of an aqueous solution of tass concentration was treated with 0.2% by weight phosphoric acid and 40%
The mixture was vigorously stirred for 15 minutes in a nitrogen gas atmosphere at tl. Distilled water equivalent to 3 parts by weight was then added to the oil. Raise the temperature to 1i:t'60Y), and continue heating for another 20 minutes. This oil was then centrifuged under the same conditions as above to separate the residual phospholipids and gum from this oil.

A portion of 5.3 kg x #) of the oil from which the gum substance was removed was treated with 85% concentrated aqueous solution and 0.05% phosphoric acid, and then placed under vacuum at an absolute pressure of 2■Hy. 40℃
The mixture was stirred for 15 minutes.

Next, Fi with the product name of Filtroll 1o5 (registered Kama trademark)
A bleaching clay commercially available from ltrol oorporat1on was used under the trade name John Manvil under the trade name FilterNicel (trade name) for oil flow rates.
A filter aid commercially available from Le Corporation was added in an amount of 0.2 - with respect to the oil flow rate, and the mixture was heated to 120 DEG C., still under vacuum, and stirred vigorously. After 20 minutes of such continued treatment, the mixture was cooled to 80° C., the vacuum was broken with nitrogen gas, and the oil was filtered through a Puchner suction funnel.

A small amount of citric acid in the form of an aqueous solution of concentrated 159I was added to bring the citric acid to 1 [IQ ppm] in the bleached oil, and the oil was then placed under vacuum at an absolute pressure of 0.2 ml if. It was subjected to steam purification/deodorization for 90 minutes at 240° C. using 17% blown steam. The oil thus obtained was named sample.

A sample for comparison was prepared as follows using a conventional alkali purification treatment method. 6. of the same twice degummed oil maintained at 40°C. a Jay was treated with 4.56% of caustic soda solution at 16° B.' and stirred vigorously for 15 minutes under nitrogen gas atmosphere. temperature t-65
℃ and continued gentle stirring for an additional 15 minutes.

This oil was then centrifuged to separate the precipitated soaps. Following this, the oil was washed twice by adding 10% by weight of hot distilled water, stirring, and centrifuging each time.
Next, this oil was placed under a vacuum with an absolute pressure of 2 Hp.
It was dried for 30 minutes at a temperature of .degree.

Add to this oil 1.0 weight percent of the same bleaching clay used previously and 0.2 weight percent of a filter aid;
Then, under an absolute pressure of 2KIIHf, the mixture was heated to 12
Bleaching was achieved by heating to 0° C. and stirring for 20 minutes. After cooling to 80°C, the oil was filtered in a P7ner suction funnel. By adding a small amount of citric acid in the form of an aqueous solution with a concentration of 15%, the degree of citric acid in the bleached oil is 110%.
The absolute pressure of this oil is 0.2
Deodorization treatment was carried out at 250° C. for 90 minutes using 1.5-degree steam blown under a vacuum of +awll If.

The oil thus obtained was named sample M.

Table 10 - Initial stage crude oil ~ 7816, 10.5458αo1.8 Degummed oil with water 75 10.8 0.158 5!
, 4 Re-explanation with 0.5 acid Gum oil 76 10.0
0.155 2x0 (j2 Physical treatment bleaching oil 151.70.18 2.50.1 Steam refining/deodorization 1 0.5 0.015 2.
5 0.1 (Sample L) Alkali treatment method Alkali treatment oil 4G 10,0 0.01
, - - Alkali treatment - bleaching oil 10 1.0
G, 05 0.4 0.1 Alkali treatment-deodorized oil 1 0.1 0.010 (L4 0.1 (Sample M) Each sample obtained by K as described above was then tested for flavor stability. Each sample was sealed in a clear 8 oz. glass bottle with 10 ounces of air space in the soil and each sample was exposed to lighting conditions using a continuous exposure device equivalent to 65 feet of candle light. It was stored for 3 weeks at a constant temperature of 35°C in a cabinet.

Samples stored in dark storage conditions were kept for 6 months at a constant temperature of 35° C. in a sealed cabinet. 1 to 9 according to the method described in Example 1 above.
Flavor evaluations were conducted by trained panel examiners using the following evaluation scales. The results are reported in Table 11.

Table 11 Sample L Sample M First 2.5 2.6
1 week after exposure storage 4.6 4.82 weeks after
4.9 4.83 weeks later 5.1
5.1 After 2 months of dark storage 2.7 5.4 After 4 months of storage
3,2 3.56 months later 4,1
4.7 Australia The strength of the scent determined by the panel test was over 99 degrees with an accuracy of 99%.

Example 5 Commercial Canadian rapeseed oil is made from several types of rapeseed oil, typically with low erucic acid and glucosyl-todo content. This oil is commercially available as a crude product degummed with water and contains residual phosphorus up to 200 ppm and erucic acid not exceeding S, O. One sample of this oil was purified in the laboratory using the method according to the invention as described below. Another sample was prepared using a conventional alkaline purification process for comparison. Some physical and chemical properties of this commercially available oil are listed in Table 12.

A 10 kg sample of this Canadian commercial grade crude rapeseed oil was placed in a metal container. An amount of maleic acid corresponding to 0.02 of the weight of oil was added in the form of an aqueous solution, keeping the temperature constant at 25° C., and the mixture was stirred for 10 minutes. Three volumes of distilled water based on the weight of oil were added and the mixture was stirred for an additional 20 minutes. The mixture was then subjected to tube centrifugation to remove hydrated phospholipids from the oil.

3.5 jcg of the thus degummed rapeseed oil was bleached in accordance with the further teachings of the present invention. The oil was maintained at 4011 under a vacuum of 2 mHp absolute and it was treated with acid in the form of 85% strength, 0.1% by weight of oil, and stirred at high power for 10 minutes. A bleaching viscosity of 0 and 3 times the weight of the oil (under the trade name of Filrol 1o5 (registered trademark))
(commercially available from Oration) and 0.6 I6 filter aid by weight of oil (filter cell)
JOhnl! with the product name (registered trademark) -Arashi nVill
Corporation) was added to the vacuumed system. The system was heated to 120° C. with vigorous stirring. After 20 minutes at this temperature, the mixture was cooled to 80° C., stirring was stopped, and the vacuum was broken with nitrogen gas. The bleached oil was then filtered in a Puchner suction funnel.

2.4# of the bleached oil thus obtained was then subjected to steam refinement II/deodorization treatment. Bleached Oil Vt
S e p was initially added in the form of an aqueous solution with a concentration of 2O4.
This oil was treated with citric acid at pm and then vacuumed at an absolute pressure of 0.2 wsHy and 4? Steam purification/deodorization was carried out in a 5-well flask for 90 minutes at 240° C. using 21 g of blown steam. The rapeseed oil thus physically refined was named Sample N. Table 12 shows some physical and chemical properties of this oil measured at various stages of the process.

A sample for comparison was treated as follows using a conventional alkali purification treatment method. 7.5 kg of rapeseed oil degummed with maleic acid as described above was
Treated with 1.391 tubes of caustic soda solution of B.
The mixture was stirred vigorously for 15 minutes at 25°C, then the temperature was raised to 65°C, and the oil was further stirred gently.The precipitated soap was then separated from the oil by centrifugation. This Oil 1 was then washed twice by adding 10% by weight of hot water and mixing, each time by separating the water by centrifugation. Following this, the oil was dried for 15 minutes at 60° C. under a vacuum of 2 fi Hf absolute pressure.
Add a layer of oil to 200ml of whitening clay [711trol C under the trade name of FILTROL 105 (registered trademark)].
0.4% by weight of oil [commercially available from Johos-Man Corporation under the trade name FilterCell®] and 0.4% by weight of oil.
This mixture was then heated to 120 DEG C. under a vacuum of absolute pressure H1 for 20 minutes.
Heated for minutes. The mixture was then cooled to 80° C., the vacuum was broken with nitrogen gas, and the oil was filtered in a vacuum funnel.

A 2.4 to 9 sample of this oil was weighed out, and 20 ppm of Kuenji was added thereto in the form of an aqueous solution. Be sure to clean this oil with a vacuum of 0.2 tmH9 for 1.
Deodorization was carried out for 90 minutes at 240 tl using 5 liters of blown steam. The alkali-treated oil thus produced was named Sample 0. Some physical and chemical properties of this oil at various stages of processing are shown in Table 12, along with those of the oil itself.

In order to evaluate the stability of the rapeseed oil thus made, these samples were tested by the N and Ol-flavor stability tests. The oil was sealed in a clear 8 oz. glass bottle with 10 air spaces above and stored and aged under low light and dark conditions. The specimens to be illuminated were heated at a constant temperature of 55° C. in an illumination cabinet with a continuous light exposure device equivalent to 65 feet of candlelight.
Selected and stored. Samples stored in the dark were kept for 8 weeks at a constant temperature of sO 0 C in a cabinet sealed against light. Flavor evaluation was performed by a trained panel of examiners. Each sample is scored for its flavor intensity on a scale of 1 to 9, with a score of 1
represents completely flavorless and a rating of 9 represents the strongest flavor.

The results obtained are shown in Table 13.

Table 13 First 2.6 2.9
After 1 week of exposure and storage 4.63.9 After 2 weeks 4.6 5. After 23 weeks
5.14.9 After 2 weeks of dark storage 2.5 After 2.94 weeks
5.0 3.26 weeks later 2.9
After 3,918 weeks 5.7 5.7 *The strength of the scent determined by the panel test is 9? Example 4: A sample of commercially available crude groundnut oil was divided into two parts, one of which was treated by the method according to the invention and the other by the conventional method for comparison. Some physical and chemical properties of the oil refining side and of the samples obtained at various stages of each refining process are listed in Table 14.

A 10# sample of crude groundnut oil was added to the weight of this oil at a rate of 2
Ls mixed with distilled water and at a concentration of 3 at 25 °C.
The mixture was vigorously stirred for 0 minutes.

The oil was then centrifuged to separate the hydrated phospholipids.

In this way, 2.8 to 9 tons of peanut oil with the gum removed
The weight of this oil in the form of an aqueous solution of l15.0.
0216 of phosphoric acid and stirred vigorously for 15 minutes at a temperature of 40° C. at atmospheric pressure. 0.5- and filter cell filter aids are also added at 0.1 to the weight of the oil, and the temperature is raised to 110°C and the mixture is stirred under vacuum at an absolute pressure of 2IEIIHt. . After stirring vigorously for 20 minutes under these conditions, the mixture was cooled to 90°C.

The vacuum was broken with nitrogen gas and the oil was filtered in a vacuum funnel.

A 2.4 # sample of this bleached oil was treated with 5 o ppm citric acid added in the form of a 20 concentration aqueous solution, and then the oil was evaporated under vacuum at 2 mHf absolute pressure. It was subjected to a 90-part steam tfH/deodorization treatment at 240° C. using blown steam. The oil thus obtained was named Sample P.

A sample for comparison was prepared using a conventional alkali purification process as follows. 2.81 to 9 of the oil, from which the gummy matter had been removed in advance using water sonication, was treated with a 14° B·' caustic soda solution in an amount corresponding to 1.296 with respect to the weight of the oil,
Then, the oil was stirred vigorously for 15 minutes at 25°C, then the temperature was raised to 65°C, and the oil was gently stirred for 15 minutes. This oil was centrifuged to separate the precipitated soaps. Following this, the oil can be washed twice with an amount of 10% by weight of hot distilled water and separated each time by centrifugation, and finally the six oils are separated under vacuum at an absolute pressure of 2w x T11. It was dried for 15 minutes at a temperature of 60°C.

To bleach this oil, use Filtroll 105 bleach of 0.5
- and the addition of ftO,1 filter aid for the filter cell;
This was carried out by heating the mixture to 110° C. under vacuum of 2 mIlf absolute and stirring for 20 minutes. After the mixture was cooled to 90° C., the vacuum was broken with nitrogen gas and the oil was filtered in a Buchner suction funnel.

A 2.4 kg sample of this bleached oil was treated with 30 ppm citric acid added as an aqueous solution at 2044 degrees and using 1.5 ml of blown steam under vacuum at 0.2 wBF absolute pressure. Deodorization treatment was performed at 240°C for 60 minutes. The oil thus obtained was named Sample R.

Both samples were tested for color conversion and peroxide increment.The zero color conversion test was performed by storing for 6 weeks in the dark at 25°C with unrestricted head space. It was complete. These color conversion tests and peroxide measurement test III were carried out in accordance with OaB Official Methods 0f111b-45 and 01B-55, respectively. The results obtained are shown in Table 15.

Sample P Sample R Color tIII constant value Peroki Color f measured value Per ■ Initial 0.10.2 0.0 G, 70.1 0.02 weeks later 1. ! i 0j O072,10,51,
After 54 weeks 1.9 04 1.0 2,5 0
6 4.04 weeks later 241 0.8 0.8
3,1 08 7.8 Example 1 Commercially available crude, unaltered beniflora oil has typically been treated to remove gums using water.

The residual phospholipid content level of such oil is sufficiently low that it can be purified by the method according to the present invention without any additional pre-treatment. Chemical properties and those of the samples obtained at the final stage of each treatment method? Listed in Table 16. Samples of such commercially available oils
into two parts, one of which according to the method according to the invention)
, and the other was purified using a conventional alkali purification method for comparison.

A 3# sample of crude Pekiniflora oil was treated with 0.0811 phosphoric acid added in the form of a f85 chronic water bath solution and stirred for 10 minutes in air at 25°C. Add Filtrol 105 bleach and also 0.4 g of Filter Cell filtration aid per weight of oil (these have already been described), and strain the mixture vigorously under vacuum to 2 HP absolute pressure. Stir and heat to 110°C. After a period of 20 minutes (such treatment), the mixture was cooled to 80° C., quenched with evacuated nitrogen gas and filtered in an oil t-puchner suction funnel.

A 2.4# sample of the oil so bleached was weighed) and treated with soppm of citric acid added in the form of a 200% aqueous solution. Following this, the oil was steam-refined/deodorized for 90 minutes at 240"O under a vacuum of 0.2 days'ay absolute pressure and with 2.0" steam t'. The resulting oil was named Sample S.

A comparative sample was prepared using a conventional alkaline refining method as follows. 4.7 & 9 of crude beniflower oil 14”
Caustic soda solution of Be'4. o%? The oil was then stirred vigorously for 15 minutes at 25°C, then the temperature was raised to t-65°C, and the oil was centrifuged after further gentle stirring for 15 minutes. The soap was removed. This was followed by washing the tube twice with 10% by weight hot distilled water and centrifuging each time.

After this second water wash, the oil was dried under vacuum at 2 wHy absolute pressure in a humid environment at 60° C. for 15 minutes.

Bleaching of this oil was performed using Filtroll 105# whitening clay of 1.5- by weight of oil and also by 0.5- by weight of oil.
This was done by adding 5% filter cell filtration aid and heating the mixture to 110° C. for 20 minutes under vacuum. After cooling this mixture to t-80°C,
The vacuum was broken with nitrogen gas and filtered in an oil tube Puchner suction funnel.

A small amount of citric acid was added as a 204% aqueous solution so that the citric acid concentration in the bleached oil was SOPPm. 2 of this oil for a long time. A kg sample was deodorized for 60 minutes at 240° C. using 1.5 parts of blown steam under a vacuum of 0.2 smHy absolute pressure. The oil thus obtained was named Sample T. . . . - Both sample tubes were then tested for color conversion test F and peroxide/oxide measurements according to the methods previously described. The obtained result is the 17th
Shown in the table.

Sample B Specimen chromaticity measurement value Peroki chromaticity measurement value Baroki yellow Red Size 8- Yellow Red Side value first L90.2
[100,? Oj O, -02 weeks later 2.
4 0.4 L4 1.5 0.2 2;
After 44 weeks 2.4 0.4 7A 1.9
0,2 7.86 weeks later 2.2 0.5 1
J 1.7 0,2 17.88 weeks later 2,
0 0,5 25β 1,4 0,2 25.9
Other features, advantages, and various embodiments of the present invention will be apparent to those skilled in the art after reviewing the foregoing description of this specification. Specific examples include hair that falls within the subject matter recited in the claims of the present application unless otherwise specified.Furthermore, although specific embodiments of the present invention have been described in detail above, various examples of these embodiments may be used. It goes without saying that variations and modifications can be made without departing from the technical scope of this specification and its claims.

Claims (1)

[Scope of Claims] (1) In order to provide a product with good oxidation stability, flavor stability, and low temperature test stability, an equivalent amount of crude vegetable oil tube refining is carried out at each of the following process steps, namely: (b) To remove the gummy substance from crude oils and fats, (1) to make a mixture by combining such crude oils and fats with a small amount of water, (厘) to stir this mixture, and (shu) to separate the oils and fats from water. (1) The above process step (a) - (removal of gummy matter/metal content from the oil obtained in Shu, from which gummy matter has been removed) (1) Combine small amounts of all suitable known degumming agents to form a mixture, stir this mixture, combine the mixture with a small amount of water, and stir the resulting mixture. , and (η fats and oils t- carried out by separating from residual impurities, B1 above (4-(η process step, gummy removal/metal removal treatment) (1) Add at least 1 weight of Vloo to the above oil or fat.
phosphoric acid in an aqueous solution such that a mixture containing (i.e. 0.02- or more) phosphoric acid is formed. (菖) This mixture is maintained at a suitable temperature to allow the reaction while stirring vigorously, and (to) the mixture treated in the process step of (iii) above is added to the mixture treated in the process step (iii) above. (The amount of phosphorus derived from the phosphoric acid added in step 11) Combine bleaching agents in a proportion that allows a residual level of up to sp ppm in the final product. raising the temperature of the mixture obtained under vacuum to a temperature suitable for the action of the bleach selected above and maintaining this temperature while stirring the mixture; (V) (c) - cooling the temperature of the mixture in the process step of (a) to a temperature such that the vacuum can be broken; and (2) subjecting the bleached fat to fW; (2) Good oxidation stability, flavor stability, and low temperature test stability. In order to provide a product with a high level of properties, an amount equivalent to the purification of crude vegetable oils and fats is required at each of the following process steps, namely (a) removal of gummy matter from the crude oils and fats. (II) stir this mixture; and (1) carry out a process to separate fats and oils from water and precipitate impurities; (ii) carry out the steps of (I-Fil) above Bleaching the fat obtained in step (1) Add at least 2/10 of 1 weight ts to the above fat.
0 (i.e., greater than 0.02 phosphoric acid) in the form of an aqueous solution, and the mixture is heated under vigorous stirring at a suitable temperature to permit the reaction. maintained at The prefecture whitening agents are combined in proportions that allow for residual levels, and the temperature of the mixture obtained in step (E=)-(1) above is raised under vacuum to obtain (1) Bring the temperature of the mixture in process steps 1) to (g) above to a temperature that is consistent with the action of the bleach and maintain this temperature while stirring the mixture; The bleached fats and oils obtained in the process steps of (■) are then subjected to steam purification and deodorization. A method for refining the above-mentioned fats and oils, including each process step. Each of the following process steps, namely (a) removal of gummy matter/metal content from the crude oil and fat, is carried out by (1) combining a small amount of a suitable known gum remover with the above oil and fat to form a mixture, ([1 Stir this mixture, (I) Combine this mixture with a small amount of water, and optionally carry out bleaching of the fats and oils obtained in process steps (-f)-(Vl above) (1) ) Add at least 2/10 of 1 layer to the above fats and oils.
0 (i.e., 0.02 or more) of phosphoric acid in the form of an aqueous solution, (1) stirring the mixture vigorously while allowing the reaction to occur; Maintained at a suitable temperature, (厘) the phosphorus content in the final product derived from the phosphoric acid added in (t-)-(1) above to the mixture treated in process steps (b)-(III) above. spp in
Combine the bleaching agents in such proportions as to permit a residual level of up to Bring the temperature to a temperature suitable for the action of the bleach and maintain this temperature while stirring the mixture; The bleaching process is carried out by cooling the bleached product to a temperature such that it can be released, and then applying the bleached oil to the bleached product. A method for refining the above-mentioned fats and oils, which includes the steps of steam purifying and deodorizing the fats and oils. In refining the oil, the following process steps are carried out: (a) bleaching of the crude oil and fat;
(i.e., at least 0.02 g) of phosphoric acid in the form of an aqueous solution, and (1) heating the mixture to a suitable temperature If while stirring vigorously to permit the reaction. 5 ppm of phosphorus in the final product derived from the phosphoric acid added to the mixture treated in the process step (a)-(1) above (ii).
Combine the bleaching agents in such proportions as to permit the residual level in step i, and (transfer) the mixture obtained in process step II above.
(V) Raise the temperature under vacuum to a temperature suitable for the action of the bleach selected above, and maintain this temperature while stirring the mixture; (The temperature of the mixture in the process step of the piece is cooled to a temperature K at which the vacuum can be released, and the bleached oil and fat is treated with P.) Above (a) - (VD The above method for refining fats and oils, which includes the steps of steam purifying and deodorizing the bleached fats and oils obtained in the process steps of (5) Claims 1, 2, or 3 of the claims.
5℃ to 20℃ for each process step in (a)
A method according to any one of the preceding claims, carried out at temperatures up to -. (6) Claims 1 to 4, wherein the bleaching step is carried out at a temperature between 90°C and 120°C.
How to follow any of the sections. (7) The phosphoric acid added in the bleaching process is 1I
I%(7)2/100 (34]chio, o24) to 2
A process according to any of the preceding claims, which is sufficient to form a mixture containing up to 710% phosphoric acid by weight.