JPH0762385A - Extracting method for fatty acid - Google Patents
Extracting method for fatty acidInfo
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- JPH0762385A JPH0762385A JP5213089A JP21308993A JPH0762385A JP H0762385 A JPH0762385 A JP H0762385A JP 5213089 A JP5213089 A JP 5213089A JP 21308993 A JP21308993 A JP 21308993A JP H0762385 A JPH0762385 A JP H0762385A
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- fatty acid
- pressure
- supercritical fluid
- temperature
- hydrolysis
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Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は脂肪酸の抽出方法に関
し、さらに詳しくは動植物組織等の天然脂質原料から高
効率で脂肪酸を抽出することができる脂肪酸の抽出方法
に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for extracting a fatty acid, and more particularly to a method for extracting a fatty acid capable of efficiently extracting a fatty acid from a natural lipid raw material such as animal and plant tissues.
【０００２】[0002]
【従来の技術】脂肪酸は、動植物、魚類、微生物等の幅
広い天然資源から得られ、食用（食用油、バター等）、
医療用（あまに油、ひまし油、軟膏、成人病予防薬
等）、香粧品用（セッケン、パーム油等）、化学工業用
（ろうそく、潤滑油、塗料、燃料等）などの種々の分野
に使用されている。BACKGROUND OF THE INVENTION Fatty acids are obtained from a wide range of natural resources such as animals, plants, fish and microorganisms, and are used for food (edible oil, butter, etc.),
Used in various fields such as medical use (linseed oil, castor oil, ointment, adult disease preventives, etc.), cosmetics (soap, palm oil, etc.), chemical industry (candles, lubricants, paints, fuels, etc.) Has been done.
【０００３】動植物等の天然原料から脂肪酸を分離する
際には、まず、天然原料を粉砕した後、クロロホルム、
ジエチルエーテル等の抽出溶媒中で攪拌、圧搾するなど
の方法により、原料中のタンパク質や有機色素から脂質
が分離される。例えば、液体燃料に変換し得る炭化水素
を生産することが知られる Botryococcus braunii は、
細胞の粉砕後、抽出溶媒であるベンゼンで抽出され、炭
化水素を含む脂質として粗分離される（ FEINBERG D.A:
Fuel Options from Microalgae with Representative
Chemical Compositions : USDOE Rep.: No. SERI-TR-23
1-2427，30 (1984) ）。When separating fatty acids from natural raw materials such as animals and plants, first, the natural raw materials are crushed and then chloroform,
Lipids are separated from the proteins and organic pigments in the raw material by a method such as stirring and squeezing in an extraction solvent such as diethyl ether. For example, Botryococcus braunii, known to produce hydrocarbons that can be converted to liquid fuels,
After crushing the cells, they are extracted with benzene as an extraction solvent and roughly separated as lipids containing hydrocarbons (FEINBERG DA:
Fuel Options from Microalgae with Representative
Chemical Compositions: USDOE Rep .: No. SERI-TR-23
1-2427, 30 (1984)).
【０００４】天然原料から粗分離された脂質は、次に加
水分解により脂肪酸とグリセリンに分解され、該加水分
解液中の脂肪酸は抽出溶媒で抽出するか、または比重の
大きいグリセリンと比較的比重の小さい脂肪酸を二層に
分けて分離することにより得られる。加水分解の方法と
しては、(1) アルキルベンゼンスルホン酸を分解試薬と
して使用し、常圧解放缶で分解するTwitchell 法、(2)
１８５０年代から行なわれている最も古い脂質分解法の
ひとつである、酸化亜鉛等の触媒によりバッチ式で分解
を行う中圧分解法、(3) 高温高圧条件下で脂質を無触媒
で分解する高圧分解法（工業的には連続的に分解槽に水
を注入して分解する）、(4) 脂質を高アルカリ下で加水
分解し、一旦脂肪酸をナトリウムまたはカリウム塩とし
て溶媒抽出してから強酸で中和し、脂肪酸を得るケン化
分解法、(5) 動物の内蔵や植物種子から抽出したリパー
ゼにより脂質を酵素分解する酵素分解法等が知られてい
る。The lipid roughly separated from the natural raw material is then hydrolyzed to be decomposed into fatty acid and glycerin, and the fatty acid in the hydrolyzed solution is extracted with an extraction solvent or has a relatively high specific gravity with glycerin having a large specific gravity. It is obtained by separating small fatty acids in two layers. As the hydrolysis method, (1) Twitchell method using alkylbenzene sulfonic acid as a decomposition reagent and decomposing in an atmospheric pressure release can, (2)
One of the oldest lipid decomposition methods that has been performed since the 1850's, medium pressure decomposition method that decomposes in batch with a catalyst such as zinc oxide, (3) high pressure that decomposes lipids without catalyst under high temperature and high pressure conditions Decomposition method (industrialally, water is continuously injected into a decomposition tank to decompose), (4) Lipids are hydrolyzed in a highly alkaline state, and fatty acids are once extracted as a sodium or potassium salt with a solvent and then with a strong acid. Known are saponification and decomposition methods for neutralizing fatty acids, and (5) enzymatic decomposition method for enzymatically decomposing lipids with lipase extracted from animal internal organs or plant seeds.
【０００５】しかしながら、脂質を加水分解した後、該
加水分解液から脂肪酸を取得する上記従来の方法では、
加水分解に長時間を要したり、製品の精製度や脂肪酸と
グリセリンの分離効率に劣るという問題があった。特に
(1) の方法では、操作が簡単で設備費も安価であるが、
分解時間が１８〜２４時間と長く、脂肪酸が空気酸化を
受けやすく製品着色度が高い。(3) の方法では、脂肪酸
とグリセリンの分離は分解塔底部から脂肪酸を取り出す
比重差を利用した方法であるため、脂肪酸とグリセリン
の完全分離は困難であった。(4) の方法は、少量の脂肪
酸を簡単に得ることができ、化粧品原料として乳化剤と
なるセッケンの製造に用いられる方法であるが、脂肪酸
とグリセリンの分離を溶媒抽出により行うため、大規模
な工業化は困難で、用途が限られている。さらに(5) の
方法も現在実用化に至っている方法であるが、反応時
間、分解率、酵素生産コスト等に問題がある。However, in the above-mentioned conventional method of obtaining fatty acids from the hydrolyzed liquid after hydrolyzing lipids,
There are problems that it takes a long time to hydrolyze and that the degree of purification of the product and the efficiency of separating fatty acid and glycerin are poor. In particular
The method (1) is easy to operate and inexpensive in equipment cost.
The decomposition time is as long as 18 to 24 hours, and fatty acids are easily subjected to aerial oxidation, resulting in high product coloring. In the method (3), since the fatty acid and glycerin are separated by utilizing the difference in specific gravity of taking out the fatty acid from the bottom of the decomposition tower, it is difficult to completely separate the fatty acid and glycerin. The method (4) is a method that can easily obtain a small amount of fatty acid and is used as a cosmetic raw material for the production of soap as an emulsifier.However, since the fatty acid and glycerin are separated by solvent extraction, a large-scale method is used. Industrialization is difficult and its applications are limited. Furthermore, the method (5) is also a method that has been put into practical use at present, but there are problems in reaction time, decomposition rate, enzyme production cost, and the like.
【０００６】[0006]
【発明が解決しようとする課題】本発明の目的は、天然
脂質原料から粉砕、圧搾、溶媒抽出等を経て得られる粗
脂質を、簡単な工程で、空気酸化による変性を受けず、
高効率で脂肪酸を取得することができる脂肪酸の抽出方
法を提供することにある。The object of the present invention is to obtain a crude lipid obtained by crushing, squeezing, solvent extraction or the like from a natural lipid raw material in a simple process without denaturation by air oxidation,
An object of the present invention is to provide a method for extracting a fatty acid that can obtain a fatty acid with high efficiency.
【０００７】[0007]
【課題を解決するための手段】本願で特許請求される発
明は以下の通りである。 （１）天然脂質原料から分離した脂質を、超臨界流体中
で高温高圧の条件下で加水分解し、その後、該加水分解
液から脂肪酸を抽出することを特徴とする脂肪酸の抽出
方法。 （２）脂質を二酸化炭素超臨界流体中で温度１００〜３
００℃および圧力７５〜３００ｋｇ／ｃｍ2 の条件下で
加水分解することを特徴とする（１）の脂肪酸の抽出方
法。 （３）加水分解液に、３１℃を超え２００℃以下の温度
および８０〜４００ｋｇ／ｃｍ2 の圧力条件下で二酸化
炭素超臨界流体を流入させて脂肪酸を抽出することを特
徴とする（１）の脂肪酸の抽出方法。The inventions claimed in this application are as follows. (1) A method for extracting a fatty acid, characterized in that a lipid separated from a natural lipid raw material is hydrolyzed in a supercritical fluid under conditions of high temperature and high pressure, and then a fatty acid is extracted from the hydrolyzed liquid. (2) Lipid in carbon dioxide supercritical fluid at a temperature of 100 to 3
The method for extracting a fatty acid according to (1), which comprises hydrolyzing under conditions of 00 ° C. and a pressure of 75 to 300 kg / cm 2 . (3) A fatty acid is extracted by allowing a carbon dioxide supercritical fluid to flow into the hydrolyzate at a temperature of higher than 31 ° C and lower than 200 ° C and a pressure of 80 to 400 kg / cm 2 (1) Method of extracting fatty acids from.
【０００８】本発明において加水分解される脂質には、
動植物、魚類、微生物等の天然脂質原料を粉砕、圧搾、
溶媒抽出等の工程を経て得られる粗脂質が用いられる。
本発明に用いられる超臨界流体には、抽出された脂肪酸
から抽出溶媒を除去する必要がなく、かつ製品に対する
溶媒の毒性を考慮する必要がない二酸化炭素（ＣＯ2 ）
が好ましく用いられる。該超臨界流体は、高温高圧下で
脂質を加水分解し、さらに超臨界流体の圧力および温度
を調節することによって分解された脂肪酸を選択的に溶
解する。The lipids hydrolyzed in the present invention include
Natural lipid raw materials such as animals and plants, fish, microorganisms are crushed, squeezed,
A crude lipid obtained through a process such as solvent extraction is used.
The supercritical fluid used in the present invention does not need to remove the extraction solvent from the extracted fatty acid and does not need to consider the toxicity of the solvent to the product, carbon dioxide (CO 2 ).
Is preferably used. The supercritical fluid hydrolyzes lipids under high temperature and high pressure, and further dissolves fatty acids decomposed by adjusting the pressure and temperature of the supercritical fluid.
【０００９】以下に本発明の抽出方法について説明す
る。まず、超臨界流体抽出容器に超臨界流体、油脂試料
および分解水を入れ、抽出容器内の圧力および温度を制
御して加水分解を行う。分解水の添加量は、試料の１０
〜５０重量％が好ましく、特に２０〜４０重量％が好ま
しい。抽出容器内の圧力および温度を上昇させることに
よって脂質への水の溶解度を増大させ、効率的な加水分
解を行うことが可能となる。The extraction method of the present invention will be described below. First, a supercritical fluid, an oil / fat sample, and decomposed water are put into a supercritical fluid extraction container, and hydrolysis is performed by controlling the pressure and temperature in the extraction container. The amount of decomposition water added is 10
˜50% by weight is preferred, and especially 20-40% by weight is preferred. By increasing the pressure and temperature in the extraction container, the solubility of water in the lipid can be increased and efficient hydrolysis can be performed.
【００１０】加水分解時の圧力は７５〜３００kg／cm2
が好ましく、７５〜２００kg／cm2が特に好ましい。ま
た加水分解時の温度は、目的とする脂肪酸が酸素の存在
しない状態で熱的変化を受けない温度、具体的には１０
０〜３００℃の温度が好ましく、１００〜２００℃の温
度が特に好ましい。加水分解時間は通常１〜３０時間で
あり、特に２〜１５時間が好ましく、２〜５時間がさら
に好ましい。The pressure during hydrolysis is 75 to 300 kg / cm 2
Is preferred, and 75 to 200 kg / cm 2 is particularly preferred. The temperature at the time of hydrolysis is the temperature at which the target fatty acid is not thermally changed in the absence of oxygen, specifically 10
A temperature of 0 to 300 ° C is preferable, and a temperature of 100 to 200 ° C is particularly preferable. The hydrolysis time is usually 1 to 30 hours, preferably 2 to 15 hours, more preferably 2 to 5 hours.
【００１１】超臨界流体抽出容器には、高温高圧となっ
た抽出容器内に分解水を圧入する系（注入口は通常抽出
容器の上部に設置される）および加水分解の副産物であ
るグリセリンを排出する系（排出口は通常抽出容器の底
部に設置される）を設け、分解水を注入しながら副産物
を簡易的に除去しつつ加水分解を行ってもよい。これに
より加水分解反応の平衡を解消することができ、分解を
促すことができる。In the supercritical fluid extraction container, a system for injecting decomposed water into the extraction container, which has been heated to high temperature and high pressure (the inlet is usually installed at the upper part of the extraction container), and glycerin which is a by-product of hydrolysis are discharged. It is also possible to provide a system (a discharge port is usually installed at the bottom of the extraction container) for performing hydrolysis while injecting decomposition water and simply removing by-products. Thereby, the equilibrium of the hydrolysis reaction can be canceled and the decomposition can be promoted.
【００１２】加水分解が終了した後、抽出容器内の圧力
をさらに上昇させて超臨界流体を添加し、脂肪酸を溶解
させて抽出する。抽出時の圧力は１００〜４００kg／cm
2 が好ましく、１５０〜３００kg／cm2 が特に好まし
い。また抽出温度は、目的とする脂肪酸が酸素の存在し
ない状態で熱的変化を受けない温度、具体的には３１を
超え２００℃以下の温度が好ましく、３１を超え１００
℃の温度が特に好ましい。抽出時間は５分〜４時間が好
ましく、特に３０分〜３時間が好ましい。超臨界流体に
は、分解された脂肪酸のみを選択的に溶解させる目的で
メタノール、Ｎ−ヘキサン、アセトニトリル等の溶媒を
エントレーナーとして混合することができる。After the hydrolysis is completed, the pressure inside the extraction vessel is further increased to add a supercritical fluid to dissolve the fatty acid for extraction. The pressure during extraction is 100-400kg / cm
2 is preferable, and 150 to 300 kg / cm 2 is particularly preferable. The extraction temperature is preferably a temperature at which the target fatty acid is not thermally changed in the absence of oxygen, specifically, a temperature of more than 31 and 200 ° C. or less, preferably more than 31 and 100.
A temperature of ° C is particularly preferred. The extraction time is preferably 5 minutes to 4 hours, and particularly preferably 30 minutes to 3 hours. A solvent such as methanol, N-hexane, or acetonitrile can be mixed in the supercritical fluid as an entrainer for the purpose of selectively dissolving only the decomposed fatty acid.
【００１３】[0013]
【作用】天然脂質原料から得られる粗脂質を超臨界流体
中の高温高圧下で加水すると分解して脂肪酸とグリセリ
ンとなる。抽出容器をさらに高圧にして超臨界流体を該
抽出容器内に流入することにより脂肪酸のみが超臨界流
体に溶解し、回収容器側に回収される。[Function] When a crude lipid obtained from a natural lipid raw material is hydrolyzed in a supercritical fluid under high temperature and high pressure, it is decomposed into a fatty acid and glycerin. The fatty acid alone is dissolved in the supercritical fluid by raising the pressure of the extraction container to a higher pressure and flowing the supercritical fluid into the extraction container, and the fatty acid is recovered in the recovery container side.
【００１４】[0014]
実施例１ 超臨界流体抽出容器にオレイン酸４００mgとグリセリン
５００mgを入れ、温度７０℃、圧力２００kg／cm2 の条
件でＣＯ2 超臨界流体を２ml／min の流速で抽出容器に
流入し、２時間抽出を行なった。回収容器には、オレイ
ン酸３５５ｇが回収され、抽出容器には４７２mgのグリ
セリンが残留していた。Example 1 400 mg of oleic acid and 500 mg of glycerin were put into a supercritical fluid extraction container, and CO 2 supercritical fluid was flowed into the extraction container at a flow rate of 2 ml / min under the conditions of temperature 70 ° C. and pressure 200 kg / cm 2 for 2 hours. Extraction was performed. 355 g of oleic acid was recovered in the recovery container, and 472 mg of glycerin remained in the extraction container.
【００１５】実施例２ Spirulina sp. 藻体１ｇ（乾燥重量）を細胞破砕し、窒
素雰囲気下で粗脂質をクロロホルム抽出した。得られた
脂質約２００mgと約１００mgの分解水を超臨界流体抽出
容器に入れ、容器内をＣＯ2 超臨界流体でみたし、雰囲
気温度１５０℃、圧力１００kg／cm2 とした。４時間
後、圧力を２００kg／cm2 に上げたＣＯ2超臨界流体を
２ml／min の流速で容器に流入したところ、ＣＯ2 排出
口側の回収容器に脂肪酸が約１４０mg回収された。Example 2 Spirulina sp. 1 g (dry weight) of algal cells were crushed into cells, and crude lipids were extracted with chloroform under a nitrogen atmosphere. About 200 mg and about 100 mg of the obtained lipid were placed in a supercritical fluid extraction container, and the inside of the container was filled with CO 2 supercritical fluid, and the atmosphere temperature was 150 ° C. and the pressure was 100 kg / cm 2 . After 4 hours, when a CO 2 supercritical fluid whose pressure had been raised to 200 kg / cm 2 was flown into the container at a flow rate of 2 ml / min, about 140 mg of fatty acid was recovered in the recovery container on the CO 2 outlet side.
【００１６】実施例３ 超臨界流体抽出容器にトリオレイン７６０mgを入れ、温
度２５０℃、圧力８０kg／cm2 の条件でＣＯ2 超臨界流
体を流通させた。同時に水を０．５ml／min で１min 、
次いで０．０１ml／min で添加し、３時間加水分解を行
った。次に容器内温度を７０℃に下げ、圧力は２００kg
／cm2 に上げ、ＣＯ2 超臨界流体を２ml／min で２時間
流通させた。ＣＯ2 排出口の回収容器には、オレイン酸
約７００mgが回収され、抽出容器にはグリセリン水が残
留していた。Example 3 760 mg of triolein was placed in a supercritical fluid extraction container, and a CO 2 supercritical fluid was circulated under the conditions of a temperature of 250 ° C. and a pressure of 80 kg / cm 2 . At the same time, water at 0.5 ml / min for 1 min,
Then, 0.01 ml / min was added and hydrolysis was carried out for 3 hours. Next, the temperature inside the container is lowered to 70 ° C and the pressure is 200 kg.
/ Cm 2 and CO 2 supercritical fluid was passed at 2 ml / min for 2 hours. About 700 mg of oleic acid was recovered in the recovery container at the CO 2 outlet, and glycerin water remained in the extraction container.
【００１７】実施例４ 超臨界流体抽出容器にトリオレイン６５０mgを入れ、温
度２００℃、圧力８０kg／cm2 の条件でＣＯ2 超臨界流
体を流通させた。同時に水を０．５ml／min で１min 、
次いで０．０１ml／min で添加し、３時間加水分解を行
った。次に容器内温度を７０℃に下げ、圧力は２００kg
／cm2 に上げ、ＣＯ2 超臨界流体を２ml／min で２時間
流通させた。ＣＯ2 排出口の回収容器には、オレイン酸
約２３０mgが回収され、抽出容器にはグリセリン水が残
留していた。Example 4 650 mg of triolein was placed in a supercritical fluid extraction vessel, and a CO 2 supercritical fluid was circulated under the conditions of a temperature of 200 ° C. and a pressure of 80 kg / cm 2 . At the same time, water at 0.5 ml / min for 1 min,
Then, 0.01 ml / min was added and hydrolysis was carried out for 3 hours. Next, the temperature inside the container is lowered to 70 ° C and the pressure is 200 kg.
/ Cm 2 and CO 2 supercritical fluid was passed at 2 ml / min for 2 hours. About 230 mg of oleic acid was recovered in the recovery container at the CO 2 outlet, and glycerin water remained in the extraction container.
【００１８】実施例５ 超臨界流体抽出容器にトリオレイン７６０mgを入れ、温
度２５０℃、圧力８０kg／cm2 の条件でＣＯ2 超臨界流
体を流通させた。同時に水を０．５ml／min で１min 、
次いで０．０１ml／min で添加し、５時間加水分解を行
った。次に容器内温度を７０℃に下げ、圧力は２５０kg
／cm2 に上げ、ＣＯ2 超臨界流体を２ml／min で２時間
流通させた。ＣＯ2 排出口の回収容器には、オレイン酸
約７００mgが回収され、抽出容器にはグリセリン水が残
留していた。Example 5 760 mg of triolein was placed in a supercritical fluid extraction vessel, and a CO 2 supercritical fluid was circulated under the conditions of a temperature of 250 ° C. and a pressure of 80 kg / cm 2 . At the same time, water at 0.5 ml / min for 1 min,
Then, 0.01 ml / min was added and hydrolysis was carried out for 5 hours. Next, the temperature inside the container is lowered to 70 ° C and the pressure is 250 kg.
/ Cm 2 and CO 2 supercritical fluid was passed at 2 ml / min for 2 hours. About 700 mg of oleic acid was recovered in the recovery container at the CO 2 outlet, and glycerin water remained in the extraction container.
【００１９】実施例６ 超臨界流体抽出容器にトリオレイン７６０mgを入れ、温
度２５０℃、圧力２００kg／cm2 の条件でＣＯ2 超臨界
流体を流通させた。同時に水を０．５ml／minで１min
、次いで０．０１ml／min で添加し、３時間加水分解
を行った。次に容器内温度を７０℃に下げ、圧力は２０
０kg／cm2 に維持し、ＣＯ2 超臨界流体を２ml／min で
２時間流通させた。ＣＯ2 排出口の回収容器には、オレ
イン酸約７００mgが回収され、抽出容器にはグリセリン
水が残留していた。Example 6 760 mg of triolein was placed in a supercritical fluid extraction vessel, and a CO 2 supercritical fluid was circulated under the conditions of a temperature of 250 ° C. and a pressure of 200 kg / cm 2 . Simultaneously with water at 0.5 ml / min for 1 min
Then, 0.01 ml / min was added and hydrolysis was carried out for 3 hours. Next, the temperature inside the container is lowered to 70 ° C. and the pressure is set to 20.
Maintaining 0 kg / cm 2 , a CO 2 supercritical fluid was passed at 2 ml / min for 2 hours. About 700 mg of oleic acid was recovered in the recovery container at the CO 2 outlet, and glycerin water remained in the extraction container.
【００２０】比較例１ 超臨界流体抽出容器にトリオレイン７６０mgを入れ、温
度２５０℃、圧力８０kg／cm2 の条件でＣＯ2 超臨界流
体を流通させた。同時に水を０．５ml／min で１min 、
次いで０．０１ml／min で添加し、３時間加水分解を行
った。次に容器内温度を７０℃に下げ、圧力は８０kg／
cm2 に維持し、ＣＯ2 超臨界流体を２ml／min で２時間
流通させた。ＣＯ2 排出口の回収容器には回収物はほと
んどなく、抽出容器にオレイン酸とグリセリン水が残留
していた。Comparative Example 1 760 mg of triolein was placed in a supercritical fluid extraction vessel, and a CO 2 supercritical fluid was circulated under the conditions of a temperature of 250 ° C. and a pressure of 80 kg / cm 2 . At the same time, water at 0.5 ml / min for 1 min,
Then, 0.01 ml / min was added and hydrolysis was carried out for 3 hours. Next, the temperature inside the container was lowered to 70 ° C and the pressure was 80 kg /
The supercritical fluid of CO 2 was flowed at 2 ml / min for 2 hours while being maintained at cm 2 . There was almost no collected material in the collection container at the CO 2 outlet, and oleic acid and glycerin water remained in the extraction container.
【００２１】[0021]
【発明の効果】本発明の脂肪酸の抽出方法によれば、同
一容器内で脂質の加水分解と得られた脂肪酸の分離を超
臨界流体中で一工程で行うことができるため、脂肪酸、
特に付加価値の高い不飽和脂肪酸を空気酸化による変性
を受けることなく、高効率で取得することができる。EFFECTS OF THE INVENTION According to the method for extracting fatty acids of the present invention, the hydrolysis of lipids and the separation of the obtained fatty acids can be carried out in one step in a supercritical fluid in the same container.
In particular, unsaturated fatty acids having high added value can be obtained with high efficiency without being modified by air oxidation.
Claims (3)
界流体中で高温高圧の条件下で加水分解し、その後、該
加水分解液から脂肪酸を抽出することを特徴とする脂肪
酸の抽出方法。1. A method for extracting a fatty acid, which comprises hydrolyzing a lipid separated from a natural lipid raw material under a condition of high temperature and high pressure in a supercritical fluid, and then extracting a fatty acid from the hydrolyzed liquid.
００〜３００℃および圧力７５〜３００ｋｇ／ｃｍ2 の
条件下で加水分解することを特徴とする請求項１記載の
脂肪酸の抽出方法。2. A lipid at a temperature of 1 in a carbon dioxide supercritical fluid.
The method for extracting a fatty acid according to claim 1, wherein the hydrolysis is performed under the conditions of 00 to 300 ° C. and a pressure of 75 to 300 kg / cm 2 .
下の温度および８０〜４００ｋｇ／ｃｍ2 の圧力条件下
で二酸化炭素超臨界流体を流入させて脂肪酸を抽出する
ことを特徴とする請求項１記載の脂肪酸の抽出方法。3. A fatty acid is extracted by allowing carbon dioxide supercritical fluid to flow into the hydrolyzate at a temperature of more than 31 ° C. and not more than 200 ° C. and a pressure of 80 to 400 kg / cm 2. Item 1. A method for extracting a fatty acid according to item 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5213089A JP2538753B2 (en) | 1993-08-27 | 1993-08-27 | How to extract fatty acids |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5213089A JP2538753B2 (en) | 1993-08-27 | 1993-08-27 | How to extract fatty acids |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH0762385A true JPH0762385A (en) | 1995-03-07 |
| JP2538753B2 JP2538753B2 (en) | 1996-10-02 |
Family
ID=16633382
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5213089A Expired - Fee Related JP2538753B2 (en) | 1993-08-27 | 1993-08-27 | How to extract fatty acids |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2538753B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6938672B2 (en) | 2003-04-24 | 2005-09-06 | Chun Pyo Hong | Rheoforming apparatus |
| US6942009B2 (en) | 2003-04-24 | 2005-09-13 | Chun Pyo Hong | Apparatus for manufacturing billet for thixocasting |
| US7514575B2 (en) | 2005-05-06 | 2009-04-07 | Battelle Energy Allicance, Llc | Production of biodiesel using expanded gas solvents |
| US7691270B2 (en) | 2005-07-13 | 2010-04-06 | Battelle Energy Alliance, Llc | Method for removing impurities from an impurity-containing fluid stream |
| US8308954B2 (en) | 2008-09-25 | 2012-11-13 | Battelle Energy Alliance, Llc | Methods for recovering a polar solvent from a fluid stream contaminated with at least one polar impurity |
| US8747673B2 (en) | 2008-09-25 | 2014-06-10 | Battelle Energy Alliance, Llc | Methods for recovering a solvent from a fluid volume and methods of removing at least one compound from a nonpolar solvent |
| JP2020103277A (en) * | 2010-04-27 | 2020-07-09 | キベルディ インコーポレイテッドＫｉｖｅｒｄｉ，Ｉｎｃ． | Use of oxyhydrogen microorganisms for the recovery and conversion of non-photosynthetic carbon from inorganic and/or C1 carbon sources into useful organic compounds |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5552393A (en) * | 1978-10-09 | 1980-04-16 | Krupp Gmbh | Method of treating crude vegetable fat and oil obtained from seed and germ |
| JPS60217299A (en) * | 1984-04-13 | 1985-10-30 | 日揮株式会社 | Condensation separation of highly unsaturated fatty acid or ester of same |
| JPS6121098A (en) * | 1984-07-10 | 1986-01-29 | Ajinomoto Co Inc | Preparation of enzymic reaction product |
| JPS6178899A (en) * | 1984-09-25 | 1986-04-22 | 岩谷産業株式会社 | Manufacture of oyster meat oil |
| JPS6272793A (en) * | 1985-09-26 | 1987-04-03 | バブコツク日立株式会社 | Method for concentrating and separating eicosapentaenic acidfrom fish oil |
| JPH0225447A (en) * | 1988-07-13 | 1990-01-26 | Nippon Oil & Fats Co Ltd | Production of highly unsaturated fatty acids |
-
1993
- 1993-08-27 JP JP5213089A patent/JP2538753B2/en not_active Expired - Fee Related
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5552393A (en) * | 1978-10-09 | 1980-04-16 | Krupp Gmbh | Method of treating crude vegetable fat and oil obtained from seed and germ |
| JPS60217299A (en) * | 1984-04-13 | 1985-10-30 | 日揮株式会社 | Condensation separation of highly unsaturated fatty acid or ester of same |
| JPS6121098A (en) * | 1984-07-10 | 1986-01-29 | Ajinomoto Co Inc | Preparation of enzymic reaction product |
| JPS6178899A (en) * | 1984-09-25 | 1986-04-22 | 岩谷産業株式会社 | Manufacture of oyster meat oil |
| JPS6272793A (en) * | 1985-09-26 | 1987-04-03 | バブコツク日立株式会社 | Method for concentrating and separating eicosapentaenic acidfrom fish oil |
| JPH0225447A (en) * | 1988-07-13 | 1990-01-26 | Nippon Oil & Fats Co Ltd | Production of highly unsaturated fatty acids |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6938672B2 (en) | 2003-04-24 | 2005-09-06 | Chun Pyo Hong | Rheoforming apparatus |
| US6942009B2 (en) | 2003-04-24 | 2005-09-13 | Chun Pyo Hong | Apparatus for manufacturing billet for thixocasting |
| US7514575B2 (en) | 2005-05-06 | 2009-04-07 | Battelle Energy Allicance, Llc | Production of biodiesel using expanded gas solvents |
| US7691270B2 (en) | 2005-07-13 | 2010-04-06 | Battelle Energy Alliance, Llc | Method for removing impurities from an impurity-containing fluid stream |
| US8308954B2 (en) | 2008-09-25 | 2012-11-13 | Battelle Energy Alliance, Llc | Methods for recovering a polar solvent from a fluid stream contaminated with at least one polar impurity |
| US8747673B2 (en) | 2008-09-25 | 2014-06-10 | Battelle Energy Alliance, Llc | Methods for recovering a solvent from a fluid volume and methods of removing at least one compound from a nonpolar solvent |
| JP2020103277A (en) * | 2010-04-27 | 2020-07-09 | キベルディ インコーポレイテッドＫｉｖｅｒｄｉ，Ｉｎｃ． | Use of oxyhydrogen microorganisms for the recovery and conversion of non-photosynthetic carbon from inorganic and/or C1 carbon sources into useful organic compounds |
Also Published As
| Publication number | Publication date |
|---|---|
| JP2538753B2 (en) | 1996-10-02 |
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