CN110305737B - Method for extracting fatty acid by using rice bran oil refined soapstock as raw material - Google Patents

Method for extracting fatty acid by using rice bran oil refined soapstock as raw material Download PDF

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CN110305737B
CN110305737B CN201910502421.7A CN201910502421A CN110305737B CN 110305737 B CN110305737 B CN 110305737B CN 201910502421 A CN201910502421 A CN 201910502421A CN 110305737 B CN110305737 B CN 110305737B
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fatty acid
rice bran
soapstock
bran oil
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CN110305737A (en
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黄华学
刘庚贵
刘永胜
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Hunan Huacheng Biotech Inc
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    • C—CHEMISTRY; METALLURGY
    • C11—ANIMAL OR VEGETABLE OILS, FATS, FATTY SUBSTANCES OR WAXES; FATTY ACIDS THEREFROM; DETERGENTS; CANDLES
    • C11B—PRODUCING, e.g. BY PRESSING RAW MATERIALS OR BY EXTRACTION FROM WASTE MATERIALS, REFINING OR PRESERVING FATS, FATTY SUBSTANCES, e.g. LANOLIN, FATTY OILS OR WAXES; ESSENTIAL OILS; PERFUMES
    • C11B13/00—Recovery of fats, fatty oils or fatty acids from waste materials
    • C11B13/02—Recovery of fats, fatty oils or fatty acids from waste materials from soap stock
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
    • Y02W30/00—Technologies for solid waste management
    • Y02W30/50—Reuse, recycling or recovery technologies
    • Y02W30/74—Recovery of fats, fatty oils, fatty acids or other fatty substances, e.g. lanolin or waxes

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  • Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • Wood Science & Technology (AREA)
  • Organic Chemistry (AREA)
  • Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
  • Fats And Perfumes (AREA)

Abstract

A method for extracting fatty acid by taking rice bran oil refined soapstock as a raw material comprises the following steps: (1) alcohol extraction; (2) solid-liquid separation; (3) membrane separation and refining; (4) decoloring; (5) concentrating; (6) and (5) separating acid water. The fatty acid finished product prepared by the method is white solid and is pure natural fatty acid from rice bran, the purity of the obtained fatty acid can reach 98 percent, the impurity content is low, and the final yield of the fatty acid is more than 70 percent; the invention does not need high-temperature vacuum distillation equipment, is suitable for plant extract factories, has simple production process, easy operation and realization and low production cost, and is suitable for industrial production.

Description

Method for extracting fatty acid by using rice bran oil refined soapstock as raw material
Technical Field
The invention relates to a method for extracting fatty acid, in particular to a method for extracting fatty acid by taking rice bran oil refined soapstock as a raw material.
Background
The rice bran oil fatty acid is a mixed fatty acid mainly comprising a palmitic acid-rich tertiary stearic acid having an iodine value of 8 or less and a freezing point of 52 ℃ or higher, and a commercial oleic acid having a high iodine value and a freezing point of 8 ℃ or less.
The rice bran oil fatty acid is white or yellowish solid, and can be used for preparing various fatty acid salts, chemical adjuvants, surfactants, high-grade soap, emulsifiers, mineral processing agents, mold release agents and polyurethane.
So far, no report of extracting fatty acid from rice bran oil refined soapstock by adopting plant extraction and separation technology exists.
At present, rice bran oil fatty acid manufacturers are rice bran oil refining factories, and no plant extract enterprises produce rice bran oil fatty acid. The main reasons are that the oil plants and the extraction plants are in different industries, the production equipment is completely different, and the mastered technologies are different. The production of rice bran oil fatty acid by an oil factory generally adopts a high-temperature vacuum distillation technology, and is an indispensable link for refining rice bran oil. The extraction plant does not need high-temperature vacuum evaporation equipment, and only the extraction plant related to the oryzanol and the natural ferulic acid can contact the rice bran oil fatty acid.
The oil factory mainly adopts molecular distillation technology and high-temperature vacuum distillation technology to separate the rice bran oil fatty acid.
CN201610992655 discloses a method for preparing PEG fatty acid ester surfactant from low acid value rice bran oil, which comprises extracting oil from rice bran with aqueous enzymatic method by taking rice bran, alkaline protease, activated clay, activated carbon, and PEG600 as raw materials, adding activated clay and activated carbon, and decolorizing rice bran oil; supercritical CO2The extraction technology can simplify riceThe refining process flow of the rice bran oil improves the refining rate of the rice bran oil; the rice bran oil is deacidified by adopting a molecular distillation technology. The method adopts a supercritical carbon dioxide extraction technology, has extremely high production cost, is not suitable for the production and application of medium and low-end products, prepares the fatty acid surfactant, uses excessive decolorizing substances, and has low product yield and low economic value.
CN201010542688 provides a method for decolorizing fatty acid in physical refining of rice bran oil, which solves the problem that the existing re-steaming technology cannot remove pink color of mixed fatty acid of rice bran oil by adding a proper amount of decolorizing agent into a mixed fatty acid system and then re-steaming, so that the mixed fatty acid of rice bran oil is in a light yellow color state, and the application range of the mixed fatty acid of rice bran oil is widened. The method comprises the following steps: 1. adding 0.01-0.1% of sulfuric acid with the concentration of 98%, 0.01-0.1% of phosphoric acid with the concentration of 85%, 0.05-0.25% of active carbon and 0.01-0.5% of lithium carbonate into rice bran oil mixed fatty acid according to weight percentage; 2. distilling under vacuum. The method adopts the traditional acidification and re-steaming technology, needs high-temperature vacuum distillation equipment, seriously damages the oryzanol as a main product, obviously reduces the economic value, and is not suitable for plant extract factories.
Disclosure of Invention
The technical problem to be solved by the invention is to overcome the defects in the prior art and provide the method for extracting the fatty acid by taking the rice bran oil refined soapstock as the raw material, which is suitable for plant extract plants, has the advantages of standard industrial product yield, high purity, simple production process, easy operation and realization and low production cost.
The technical scheme adopted by the invention for solving the technical problems is as follows: a method for extracting fatty acid by taking rice bran oil refined soapstock as a raw material comprises the following steps:
(1) alcohol extraction: heating and softening rice bran oil refined soapstock, adding low carbon alcohol, mixing uniformly, adjusting pH, heating and extracting, and filtering to obtain an extracting solution;
(2) solid-liquid separation: adjusting pH, filtering after the precipitate is completely precipitated, and collecting precipitate and filtrate respectively, wherein the precipitate is used for preparing oryzanol, and the filtrate is fatty acid separation liquid;
(3) membrane separation and refining: separating and refining the fatty acid separation liquid by using an organic membrane, and collecting downstream liquid with corresponding molecular weight to obtain membrane refined liquid;
(4) and (3) decoloring: adding powdered activated carbon into the membrane refined solution for decolorization, and filtering to obtain decolorized solution;
(5) concentration: vacuum concentrating the decolorized solution under reduced pressure to obtain concentrated solution;
(6) acid water separation: and cooling the concentrated solution to room temperature to separate out a large amount of white fatty acid solid, and filtering to obtain a white fatty acid solid finished product.
Preferably, in the step (1), the temperature for heating and softening the rice bran oil refining soapstock is 35-65 ℃. If the heating temperature is low, the soapstock keeps a solid hardening state and can be softened only by heating for a long time; if the heating temperature is high, the soapstock is alkaline, so that the oryzanol as the main product is obviously damaged, and the fatty acid of the product is a byproduct for producing the oryzanol.
Preferably, in the step (1), the low carbon alcohol is an aqueous solution of methanol or ethanol, the corresponding volume concentration is 80-95%, and the dosage of the low carbon alcohol is 3-6 times of the weight of the soapstock. The invention discloses that the methanol and the ethanol can extract the oryzanol as the main product and the fatty acid as the byproduct, and relatively, the fatty acid extracted from the ethanol has light color, less impurities and high purity. If the concentration of the low-carbon alcohol is low, most oryzanol cannot be extracted, the loss of main products is large, and the extraction amount of the by-product fatty acid is reduced at the same time; if the concentration of the lower alcohol is high, it is difficult to recover the high-concentration lower alcohol during the production. The dosage of the low-carbon alcohol is determined according to the content of the oryzanol as a main product, generally, the multiple quantity is increased when the content of the oryzanol is high, and the multiple quantity is reduced when the content of the oryzanol is low, and the economic benefit is considered.
Preferably, in the step (1), the substance for adjusting the pH is a sodium hydroxide aqueous solution, the corresponding mass concentration is 2-10%, and the pH is adjusted to 8-11. The sodium hydroxide aqueous solution is the most economical substance for adjusting the alkalinity, the dosage is large when the concentration is low, and the labor safety is affected by a large amount of solution heat generated in the preparation process when the concentration is high. Finally, if the pH value of the extracting solution is adjusted to be too high, the main product oryzanol can be obviously damaged, so that the yield of the oryzanol is low; too low is detrimental to the dissolution of oryzanol and also does not allow the fatty acids to form sodium salts for dissolution, resulting in low yields of both the main product and the fatty acids.
Preferably, in the step (1), the extraction heating temperature is 50-65 ℃, and the extraction time is 10-40 min. If the heating temperature is high or the extraction time is long, the oryzanol serving as a main product is obviously damaged under the alkaline condition, and the fatty acid is easy to generate complex reaction to reduce the yield; if the temperature is low or the extraction time is short, the dissolution of the main product and the fatty acid is not favorable.
Preferably, in the step (1), the filtration mode is sedimentation centrifugation or disc centrifugation or tubular centrifugation. The three modes can be used for separating the extracting solution containing main and side products from the extracting slag on the premise of obtaining clear filtrate.
Preferably, in the step (2), the substance for adjusting the pH is a hydrochloric acid or sulfuric acid aqueous solution, the corresponding mass concentration is 5-20%, and the pH is adjusted to 6.5-7.5. The hydrochloric acid and the sulfuric acid aqueous solution can be used for adjusting the pH value of the alkaline solution to be neutral or acidic in production, have wide application range and do not generate chemical reaction with main products. The dosage is large when the concentration is low, and the preparation process generates a large amount of solution heat and is not beneficial to labor safety when the concentration is high. Finally, if the pH is adjusted to be too low, a large amount of fatty acid is attached to the oryzanol serving as a main product, so that the oryzanol is not purified easily, and the yield of the fatty acid is reduced remarkably; if the pH value is too high, the main product is not completely separated out, the yield is low, and the separation and purification of the fatty acid are not facilitated.
Preferably, in the step (2), the time for complete precipitation is 2-12 h. If the precipitation time is short, the oryzanol as the main product is incompletely precipitated, the yield is reduced, and the separation and purification of the fatty acid are obviously influenced due to the mixing of the main product; if the precipitation time is long, the production period is affected, and the production efficiency is reduced.
Preferably, in the step (2), the filtration mode is suction filtration or sedimentation centrifugation or tubular centrifugation or disc centrifugation. The filtration mode is determined according to the product properties, and if the precipitate is well dispersed, suction filtration is selected; or the sediment with oil viscosity is filtered by tubular centrifugation or disc centrifugation.
Preferably, in the step (3), the molecular weight cut-off of the organic membrane is 1 KD-3 KD. If the molecular weight cut-off is too low, fatty acid and pigment are mixed together, and the amount of fatty acid remained in the upstream liquid of the membrane is large, so that the yield is obviously influenced; if the molecular weight cut-off is too large, a good decoloring effect cannot be achieved, and decoloring and purification of fatty acid are not facilitated.
Preferably, in the step (4), the added amount of the powdered activated carbon is 0.2-0.5% of the weight of the membrane refining liquid. If the addition amount of the activated carbon is large, the fatty acid is adsorbed and lost, and the production cost is increased; or the decoloring effect is poor when the addition amount is small.
Preferably, in the step (4), the filtration mode is plate-frame filtration or tube centrifugation. The filtering precondition is that the active carbon powder can be completely removed. In general, plate-frame filtration and tubular centrifugation can achieve the purpose.
Preferably, in the step (5), the concentration mode is vacuum reduced pressure concentration, the concentration vacuum degree is-0.08 to-0.09 MPa, the temperature is 55 to 65 ℃, and the concentration degree is 20 to 25 Baume degrees. The vacuum concentration condition has the obvious advantages of high concentration speed and no damage to fatty acid components. When the concentration degree reaches the corresponding Baume degree, the fatty acid content is high, the water content is low, and the fatty acid is easy to separate out when the mixed solution system reaches the normal temperature.
Preferably, in the step (6), the concentrated solution is naturally cooled or refrigerated at 0-5 ℃, and the filtration is sedimentation and centrifugation. The precipitation speed is slow by natural cooling and precipitation is slightly fast by refrigeration, thus being suitable for conditional factories. Because there is little water after the fatty acid is separated out, the separation of the fatty acid and the water can be realized by sedimentation and centrifugation.
The principle of the invention is as follows: the invention uses rice bran oil refined soapstock as raw material to extract fatty acid. The raw material soapstock mainly contains the main product oryzanol, the by-product fatty acid and other impurities, and the fatty acid is extracted and separated as the by-product in the process of extracting the main product oryzanol, so that the method has the remarkable advantage of low production cost and realizes the comprehensive utilization of the raw materials. By utilizing the property that the oryzanol as the main product, the fatty acid as the byproduct and most impurities can be dissolved in the alkaline low-carbon alcohol, the main and the secondary products are extracted by utilizing the high-carbon low-carbon alcohol by adjusting the proper pH value. The oryzanol as the main product is insoluble in acidic low-carbon alcohol, the fatty acid as the byproduct is soluble in acidic low-carbon alcohol, the oryzanol can be precipitated and the fatty acid can be kept in the acidic low-carbon alcohol solution by adjusting proper pH, and then the separation of the main product and the auxiliary product can be realized by proper filtration. The low-carbon alcohol solution of fatty acid still contains partial impurities and pigments, and most of the impurities and pigments can be removed by selecting proper membrane molecular weight interception, and residual pigments and a small amount of impurities are further removed by adding powdered activated carbon. Finally, residual impurities are dispersed in water through concentration to a proper degree, and fatty acid is separated out in the cooling process, and then the fatty acid and the water-containing impurities are completely separated through proper filtration. The invention does not need high-temperature vacuum distillation equipment, has simple production process and easy control and realization of production, and is suitable for plant extract factories, thereby further expanding the application range.
The invention has the beneficial effects that:
(1) the fatty acid prepared according to the invention is white solid, and the purity of the obtained fatty acid can reach 98.65 percent through gas chromatography detection, the content of impurities is low, and the final yield of the fatty acid is more than 70 percent;
(2) the invention does not adopt high-temperature vacuum distillation equipment, the product fatty acid is not reddish, and is extracted and separated as a byproduct for producing the main product oryzanol, the production process is simple, the control and the realization are easy, and the invention has the obvious advantage of low production cost; can realize the comprehensive utilization of raw materials, further expand the application range and is suitable for plant extract factories.
Detailed Description
The present invention will be further described with reference to the following examples.
The rice bran oil refined soapstock used in the embodiment of the invention is purchased from Liaoning, and the content of fatty acid is 12.35%. The purity of the sodium hydroxide used in the embodiment of the invention is 98%, the mass concentration of the sulfuric acid is 98%, and the mass concentration of the hydrochloric acid is 35%. The chemical reagents and raw and auxiliary materials used in the examples of the present invention are commercially available in a conventional manner unless otherwise specified.
In the embodiment of the invention, the content of fatty acid is detected by adopting a Gas Chromatography (GC) external standard method.
Example 1
(1) Alcohol extraction: adding 400kg of soapstock raw material refined from rice bran oil into 3m3In an extraction tank, starting steam, controlling the temperature to be 45 ℃, heating for softening, adding 2000L of edible ethanol with the volume concentration of 90% after softening, stirring and mixing uniformly, adjusting the pH of a solution system to be 10 by using a sodium hydroxide aqueous solution with the mass concentration of 5%, heating, stirring and extracting for 20min at 55 ℃, settling, centrifuging and filtering while hot, and removing centrifugal precipitate to obtain an extracting solution;
(2) solid-liquid separation: adjusting the pH of the extracting solution to 7.2 by using a hydrochloric acid aqueous solution with the mass concentration of 15%, standing and precipitating for 6h, after the precipitation is complete, performing suction filtration, and respectively collecting the precipitate and filtrate, wherein the precipitate is used for preparing oryzanol, and the filtrate is a fatty acid separation solution;
(3) membrane separation and refining: separating and refining the fatty acid separation liquid by organic membrane complete equipment, selecting a roll type organic membrane with the molecular weight cutoff of 1KD, finally adding 90% edible ethanol which is 1 time of the upstream liquid for cleaning, and collecting the downstream liquid passing through the membrane to obtain nearly colorless membrane refined liquid;
(4) and (3) decoloring: adding 6kg of powdered activated carbon into the membrane refined solution for decolorization, fully and uniformly stirring at normal temperature, and filtering by using a plate frame to obtain a decolorized solution;
(5) concentration: vacuum decompression concentration is adopted, the concentration vacuum degree is-0.08 to-0.09 MPa, the temperature is 55 to 65 ℃, and the concentration is carried out to 21 Baume degrees, so as to obtain concentrated solution;
(6) acid water separation: naturally cooling the concentrated solution to room temperature to precipitate a large amount of white fatty acid solid, and settling, centrifuging and separating a small amount of water and acid to obtain 35.57kg of white fatty acid solid finished product.
The obtained fatty acid finished product is white solid, and the purity of the fatty acid is 98.35 percent and the final yield is 72 percent through gas chromatography detection.
Example 2
(1) Alcohol extraction: adding 250kg of soapstock raw material refined from rice bran oil into 3m3In an extraction tank, starting steam, controlling the temperature to be 50 ℃, heating for softening, adding 1500L of methanol with the volume concentration of 92% after softening, stirring and mixing uniformly, adjusting the pH value of a solution system to be 8.5 by using an aqueous solution of sodium hydroxide with the mass concentration of 8%, heating and stirring for extraction for 30min at 60 ℃, performing tubular centrifugal filtration while hot, and removing centrifugal precipitation to obtain an extracting solution;
(2) solid-liquid separation: adjusting the pH of the extracting solution to 6.7 by using a sulfuric acid aqueous solution with the mass concentration of 10%, standing and precipitating for 8h, precipitating and centrifuging after complete precipitation, respectively collecting precipitate and filtrate, wherein the precipitate is used for preparing oryzanol, and the filtrate is a fatty acid separation solution;
(3) membrane separation and refining: separating and refining the fatty acid separation liquid by organic membrane complete equipment, selecting a roll-type organic membrane with the molecular weight cutoff of 2KD, finally adding 92% methanol which is 1 time of the upstream liquid for cleaning, and collecting the downstream liquid passing through the membrane to obtain nearly colorless membrane refined liquid;
(4) and (3) decoloring: adding 4.5kg of powdered activated carbon into the membrane refined solution for decolorization, fully and uniformly stirring at normal temperature, and filtering by using a plate frame to obtain a decolorized solution;
(5) concentration: vacuum decompression concentration is adopted, the concentration vacuum degree is-0.08 to-0.09 MPa, the temperature is 55 to 65 ℃, and the concentration is carried out to 24 Baume degrees, so as to obtain concentrated solution;
(6) acid water separation: and (3) refrigerating the concentrated solution at 0-5 ℃, standing to room temperature to separate out a large amount of white fatty acid solids, and settling, centrifuging and separating a small amount of water and acid to obtain 23.16kg of white fatty acid solid finished products.
The obtained fatty acid finished product is white solid, and the purity of the fatty acid is 98.65% and the final yield is 75% through gas chromatography detection.

Claims (4)

1. A method for extracting fatty acid by taking rice bran oil refined soapstock as a raw material is characterized by comprising the following steps:
(1) alcohol extraction: heating and softening rice bran oil refined soapstock, adding low carbon alcohol, mixing uniformly, adjusting pH, heating and extracting, and filtering to obtain an extracting solution; the heating and softening temperature of the rice bran oil refining soapstock is 35-65 ℃; the low-carbon alcohol is an aqueous solution of methanol or ethanol, the corresponding volume concentration is 80-95%, and the dosage of the low-carbon alcohol is 3-6 times of the weight of the soapstock; adjusting the pH value by using a sodium hydroxide aqueous solution as a substance, adjusting the pH value to 8-11 according to the corresponding mass concentration of 2-10%, extracting and heating the solution at 50-65 ℃ for 10-40 min, and filtering the solution by settling centrifugation, disc centrifugation or tubular centrifugation;
(2) solid-liquid separation: adjusting pH, filtering after the precipitate is completely precipitated, and collecting precipitate and filtrate respectively, wherein the precipitate is used for preparing oryzanol, and the filtrate is fatty acid separation liquid; the substance for adjusting the pH is a hydrochloric acid or sulfuric acid aqueous solution, the corresponding mass concentration is 5-20%, and the pH is adjusted to 6.5-7.5; the time for complete precipitation is 2-12 h; the filtration mode is suction filtration or sedimentation centrifugation or tubular centrifugation or disc centrifugation;
(3) membrane separation and refining: separating and refining the fatty acid separation liquid by using an organic membrane, and collecting downstream liquid with corresponding molecular weight to obtain membrane refined liquid; the molecular weight cut-off of the organic membrane is 1 KD-3 KD;
(4) and (3) decoloring: adding powdered activated carbon into the membrane refined solution for decolorization, and filtering to obtain decolorized solution;
(5) concentration: vacuum concentrating the decolorized solution under reduced pressure to obtain concentrated solution;
(6) acid water separation: and cooling the concentrated solution to room temperature to separate out a large amount of white fatty acid solid, and filtering to obtain a white fatty acid solid finished product.
2. The method for extracting fatty acid from rice bran oil refined soapstock as a raw material according to claim 1, wherein in the step (4), the addition amount of the powdered activated carbon is 0.2-0.5% of the weight of the membrane refining liquid, and the filtration mode is plate-frame filtration or tubular centrifugation.
3. The method for extracting fatty acid from rice bran oil refined soapstock as the raw material according to claim 1 or 2, wherein in the step (5), the concentration mode is vacuum reduced pressure concentration, the concentration vacuum degree is-0.08 to-0.09 MPa, the temperature is 55 to 65 ℃, and the concentration degree is 20 to 25 Baume degrees.
4. The method for extracting fatty acid from rice bran oil refined soapstock as the raw material according to claim 1 or 2, wherein in the step (6), the concentrated solution is naturally cooled or refrigerated at 0-5 ℃, and the filtration is sedimentation and centrifugation.
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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103145789A (en) * 2013-03-26 2013-06-12 郑州良远科技有限公司 Method for extracting oryzanol from rice bran crude oil

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN103145789A (en) * 2013-03-26 2013-06-12 郑州良远科技有限公司 Method for extracting oryzanol from rice bran crude oil

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
米糠油加工最新进展;Mahua Ghosh等;《中国油脂》;20080120(第01期);全文 *
米糠油及其付产物中脂肪酸;许仁溥等;《粮食与油脂》;19930402(第01期);全文 *

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