JPH0952866A - Concentrated separation of fatty acid ester - Google Patents
Concentrated separation of fatty acid esterInfo
- Publication number
- JPH0952866A JPH0952866A JP7203445A JP20344595A JPH0952866A JP H0952866 A JPH0952866 A JP H0952866A JP 7203445 A JP7203445 A JP 7203445A JP 20344595 A JP20344595 A JP 20344595A JP H0952866 A JPH0952866 A JP H0952866A
- Authority
- JP
- Japan
- Prior art keywords
- extraction
- fatty acid
- acid ester
- fluid
- separation
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- 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
- Y02P—CLIMATE CHANGE MITIGATION TECHNOLOGIES IN THE PRODUCTION OR PROCESSING OF GOODS
- Y02P20/00—Technologies relating to chemical industry
- Y02P20/50—Improvements relating to the production of bulk chemicals
- Y02P20/54—Improvements relating to the production of bulk chemicals using solvents, e.g. supercritical solvents or ionic liquids
Landscapes
- Organic Low-Molecular-Weight Compounds And Preparation Thereof (AREA)
- Extraction Or Liquid Replacement (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は高度不飽和脂肪酸、特に
エイコサペンタエン酸（ＥＰＡ）、ドコサヘキサエン酸
（ＤＨＡ）のエステルを濃縮分離する方法に関する。TECHNICAL FIELD The present invention relates to a method for concentrating and separating highly unsaturated fatty acids, particularly esters of eicosapentaenoic acid (EPA) and docosahexaenoic acid (DHA).
【０００２】[0002]
【従来の技術】魚油等の海産物油脂に含まれるＥＰＡや
ＤＨＡは、心筋梗塞、脳梗塞等の血栓性疾患の予防及び
治療に有効であることが知られている。しかし、天然物
中の含有量は低いため、濃縮する必要がある。各種脂肪
酸エステルの混合物から特定の脂肪酸エステルを濃縮分
離する方法として蒸留法、クロマトグラフィー、超臨界
抽出方法等が知られている。ところが、蒸留による方法
は、沸点差による分離であるため、沸点が近似した高度
不飽和脂肪酸エステルと他の飽和あるいは低不飽和脂肪
酸エステルとの分離は困難であり、さらに高沸点である
ために、１ｍｍＨｇ以下の減圧下での蒸留によっても、
高温に加熱することが避けられず、このために異性化や
重合が起こり易いという欠点がある。また、クロマトグ
ラフィーによる方法では、分離に長時間を要するととも
に原料に対して大量の溶剤を必要とする等の欠点があ
る。2. Description of the Related Art EPA and DHA contained in marine oils and fats such as fish oil are known to be effective in preventing and treating thrombotic diseases such as myocardial infarction and cerebral infarction. However, its content in natural products is low, so it needs to be concentrated. Distillation, chromatography, supercritical extraction and the like are known as methods for concentrating and separating a specific fatty acid ester from a mixture of various fatty acid esters. However, since the method by distillation is a separation by boiling point difference, it is difficult to separate highly unsaturated fatty acid ester having a similar boiling point from other saturated or low unsaturated fatty acid ester, and because of the higher boiling point, Even by distillation under reduced pressure of 1 mmHg or less,
Heating at high temperature is unavoidable, which has a drawback that isomerization and polymerization are likely to occur. Further, the method by chromatography has the drawbacks that it takes a long time for separation and a large amount of solvent is required for the raw materials.
【０００３】一方、超臨界状態の流体を利用して、特定
脂肪酸成分を分離することが提案されている（特公平１
−２１８２０号公報）。この方法では、油脂中のトリグ
リセライドの超臨界状態の二酸化炭素への溶解度を高め
るために、脂肪酸アルキルエステルとした後に、二酸化
炭素によって抽出分離を行っており、さらに抽出された
脂肪酸アルキルエステルを含む二酸化炭素相を精留する
することによって濃縮分離効率を高めている。この方法
は、処理温度が低く蒸留方法に比して特定の成分の分離
特性が優れたものであるが、目的とする特定成分の濃縮
効率が充分なものではない。On the other hand, it has been proposed to separate a specific fatty acid component by using a fluid in a supercritical state (Japanese Patent Publication 1).
-21820). In this method, in order to increase the solubility of triglyceride in fats and oils in carbon dioxide in a supercritical state, after extraction with fatty acid alkyl ester, carbon dioxide is extracted and separated, and the extracted fatty acid alkyl ester-containing dioxide is added. The concentration and separation efficiency is increased by rectifying the carbon phase. This method has a low treatment temperature and is superior in the separation property of the specific component as compared with the distillation method, but the efficiency of concentrating the desired specific component is not sufficient.
【０００４】また、抽出槽上部に加熱環流部を有する方
法（特公昭５４−１０５３９号公報、特公平１−２１８
２０号公報）、抽出塔に複数の温度の異なる領域を設け
ることによって抽出塔内で分離および還流を繰り返し濃
縮分離する方法（特開昭１−２４９７４２号公報、特開
平１−２４９１０２号公報）が提案されているが、これ
らの方法は、抽出塔の正確な温度制御が必要となり装置
が複雑なものとなる。Further, a method in which a heating reflux section is provided above the extraction tank (Japanese Patent Publication No. 54-10539, Japanese Patent Publication No. 1-218).
No. 20), and a method of repeatedly concentrating and separating in the extraction tower by separating and refluxing by providing a plurality of regions having different temperatures (JP-A-1-249742, JP-A-1-249102). Although proposed, these methods require precise temperature control of the extraction column and complicate the equipment.
【０００５】[0005]
【発明が解決しようとする課題】本発明は、各種の脂肪
酸の低級アルコールエステルの混合物から効果的、経済
的に分子量によって分画化する方法を提供することを課
題とするものである。An object of the present invention is to provide a method for effectively and economically fractionating a mixture of lower alcohol esters of various fatty acids by molecular weight.
【０００６】[0006]
【課題を解決するための手段】本発明は、脂肪酸エステ
ルの濃縮分離方法において、脂肪酸エステルの混合物を
抽出槽において超臨界状態もしくは亜臨界状態の状態の
流体によって抽出分離した後に、抽出残渣を精留機能を
有する抽出塔に導入し、超臨界状態もしくは亜臨界状態
の流体を供給して抽出分離し、抽出相もしくは抽出残渣
中に特定の脂肪酸エステルを濃縮分離する濃縮分離方法
である。また、脂肪酸がエイコサペンタエン酸（ＥＰ
Ａ）又はドコサヘキサエン酸（ＤＨＡ）であり、抽出温
度が４６〜１００℃、抽出圧力が、８０〜３００気圧で
ある前記の方法である。The present invention is a method for concentrating and separating a fatty acid ester, wherein a mixture of fatty acid esters is extracted and separated by a fluid in a supercritical state or a subcritical state in an extraction tank, and then the extraction residue is refined. This is a concentration and separation method in which a fluid in a supercritical state or a subcritical state is introduced into an extraction column having a distillation function to perform extraction and separation, and a specific fatty acid ester is concentrated and separated in an extraction phase or an extraction residue. In addition, the fatty acid is eicosapentaenoic acid (EP
A) or docosahexaenoic acid (DHA), the extraction temperature is 46 to 100 ° C., and the extraction pressure is 80 to 300 atm.
【０００７】各種脂肪酸の低級アルコールエステルは、
超臨界状態もしくは亜臨界状態の二酸化炭素に溶解し、
しかもその溶解度は分子量によって変化する。低分子の
成分は溶解度が高いため、経時的に抽出処理を行った場
合優先的に抽出される。また、低分子の成分は恒温状態
では、低い抽出圧力、すなわち低い溶解能力であっても
溶解され、圧力が高いほどより大きな分子量の溜分が超
臨界あるいは亜臨界状態の二酸化炭素に溶解させること
ができるので、この性質を利用すれば通常の分子蒸留法
では分画が困難な大きな分子量を有する有機物でも容易
に効率よく分離することができる。本発明において、超
臨界状態の流体とは、温度および圧力が臨界点以上の流
体を称し、亜臨界状態の流体とは、圧力、温度の少なく
ともいずれか一方が臨界点の近傍にある臨界点を超えな
い流体であって、二酸化炭素では、圧力が７５ｋｇ／ｃ
ｍ2Ｇ 未満、温度が３１℃未満の流体を称す。Lower alcohol esters of various fatty acids are
Dissolved in carbon dioxide in the supercritical or subcritical state,
Moreover, its solubility changes depending on the molecular weight. Since low-molecular components have high solubility, they are preferentially extracted when the extraction treatment is performed over time. In addition, low-molecular weight components are dissolved under isothermal conditions even at low extraction pressures, that is, at low dissolution capacities, and the higher the pressure, the higher the molecular weight fraction that can be dissolved in supercritical or subcritical carbon dioxide. Therefore, by utilizing this property, it is possible to easily and efficiently separate even an organic substance having a large molecular weight, which is difficult to fractionate by an ordinary molecular distillation method. In the present invention, a fluid in a supercritical state refers to a fluid having a temperature and a pressure equal to or higher than a critical point, and a fluid in a subcritical state refers to a critical point in which at least one of pressure and temperature is near the critical point. A fluid that does not exceed 75 kg / c with carbon dioxide
A fluid having a temperature of less than m 2 G and a temperature of less than 31 ° C.
【０００８】ＥＰＡ、ＤＨＡの超臨界もしくは亜臨界状
態の二酸化炭素に対する溶解度と、炭素数が１８以下の
脂肪酸からなる低分子量のエステルとは溶解度差が大き
く、低級脂肪酸のエステルは大量に溶解するので、超臨
界もしくは亜臨界状態の二酸化炭素によって低分子量の
脂肪酸エステルを除去した後に、精留機能を有する抽出
塔において抽出分離することにより、抽出塔の負荷は小
さくなり、塔径が小さく、塔高が低い抽出装置によって
精製分離をすることが可能となる。精留機能を有する抽
出塔は、抽出塔に温度勾配を形成したり、環流手段等を
設けることによって得ることが可能である。また、低級
脂肪酸のエステルを分離した後に、さらにＥＰＡとＤＨ
Ａを精製分離することも可能である。また、超臨界状態
の流体として、二酸化炭素以外にも炭化水素等を用いて
も良い。There is a large difference in solubility between the solubility of EPA and DHA in carbon dioxide in the supercritical or subcritical state and the low molecular weight ester consisting of a fatty acid having 18 or less carbon atoms, and the ester of a lower fatty acid dissolves in a large amount. By removing the low molecular weight fatty acid ester with carbon dioxide in the supercritical or subcritical state and then performing extraction separation in the extraction column having a rectification function, the load on the extraction column is reduced, the column diameter is small, and the column height is high. It becomes possible to perform purification separation with an extraction device having a low power consumption. An extraction column having a rectification function can be obtained by forming a temperature gradient in the extraction column or providing a reflux means or the like. In addition, after separating the ester of lower fatty acid, EPA and DH
It is also possible to purify and separate A. In addition to carbon dioxide, hydrocarbon or the like may be used as the fluid in the supercritical state.
【０００９】[0009]
【実施例】以下実施例により、本発明を具体的に説明す
る。 実施例１ 図１に示した、内径７０ｍｍ、高さ３００ｍｍの抽出槽
１に表１に示す組成の脂肪酸エチルエステル６を１ｋｇ
／時の流量で供給した。抽出槽の外部の加温装置５に温
水を通水し、抽出槽の温度を５０℃とした。二酸化炭素
は、ボンベ２からポンプ３によって熱交換器４に供給さ
れ、５０℃に加熱した後に抽出槽に供給して抽出を行っ
た。抽出槽の圧力は弁７によって１２０ｋｇ／ｃｍ2Ｇ
に設定した。脂肪酸エチルエステルを抽出した抽出相は
減圧弁８で３０ｋｇ／ｃｍ2Ｇ まで減圧し、分離槽９で
抽出物を分離した。抽出物を分離した二酸化炭素は、ガ
スメーター１０で検量して系外に放出した。抽出物の量
は０．４ｋｇ／時であり、ＥＰＡの濃度は３〜６重量％
の範囲内にあり、ＤＨＡの濃度は、１重量％であった。The present invention will be specifically described with reference to the following examples. Example 1 1 kg of fatty acid ethyl ester 6 having the composition shown in Table 1 was placed in the extraction tank 1 having an inner diameter of 70 mm and a height of 300 mm shown in FIG.
It was supplied at a flow rate of / hour. Hot water was passed through the heating device 5 outside the extraction tank, and the temperature of the extraction tank was set to 50 ° C. Carbon dioxide was supplied from the cylinder 2 to the heat exchanger 4 by the pump 3, heated to 50 ° C., and then supplied to the extraction tank for extraction. The pressure of the extraction tank is 120 kg / cm 2 G by the valve 7.
Set to. The extraction phase from which the fatty acid ethyl ester was extracted was decompressed to 30 kg / cm 2 G by the decompression valve 8 and the extract was separated in the separation tank 9. The carbon dioxide from which the extract was separated was calibrated with a gas meter 10 and released outside the system. The amount of the extract is 0.4 kg / hour, and the concentration of EPA is 3 to 6% by weight.
, And the concentration of DHA was 1% by weight.
【００１０】次いで、抽出槽の下部より、抽出残渣１１
を０．６ｋｇ／時の流量で抜き出し、ポンプ１２で加圧
して直径３ｍｍ、長さ３ｍｍの充填物ディクソン１３を
充填した内径３０ｍｍ、高さ３ｍの抽出塔１４に供給し
た。ＥＰＡおよびＤＨＡの濃度は、それぞれ２５〜３０
重量％および１５〜２０重量％であった。抽出塔の温度
は、塔の外側に設けた６個のヒータ１５によって調節
し、上部より順に７０、６６、６２、５８、５４、５０
℃とし、下部は５０℃とした。ボンベ２からポンプ１６
で加圧して熱交換器１７において５０℃とした二酸化炭
素を流量１３．３ｋｇ／時で抽出塔に供給し、抽出およ
び精留を行った、抽出圧力は、弁１８によって、１５５
ｋｇ／ｃｍ2Ｇ に設定した。脂肪酸のエチルエステルを
抽出した抽出相は、減圧弁１９で３０ｋｇ／ｃｍ2Ｇ ま
で減圧し、分離槽２０で抽出物を分離した。抽出物を分
離した二酸化炭素は、ガスメータ２１で検量して系外に
放出した。抽出物の量は、平均０．２ｋｇ／時であり、
ＥＰＡおよびＤＨＡ濃度はそれぞれ２〜５重量％、１〜
３重量％の範囲を変化した。一方、抽出塔の下部より未
抽出物を０．４ｋｇ／時の流量で抜き出したところ、Ｅ
ＰＡおよびＤＨＡの濃度はそれぞれ、３８〜４３重量％
および２４〜２８重量％の範囲にあった。Next, from the bottom of the extraction tank, the extraction residue 11
Was extracted at a flow rate of 0.6 kg / hour, pressurized by a pump 12, and supplied to an extraction tower 14 having an inner diameter of 30 mm and a height of 3 m filled with Dickson 13 having a diameter of 3 mm and a length of 3 mm. The concentration of EPA and DHA is 25-30, respectively.
% And 15-20% by weight. The temperature of the extraction tower is adjusted by six heaters 15 provided on the outside of the tower, and 70, 66, 62, 58, 54, 50 in order from the top.
C. and the lower part was 50.degree. Cylinder 2 to pump 16
Carbon dioxide pressurized at 50 ° C. in the heat exchanger 17 was supplied to the extraction column at a flow rate of 13.3 kg / hour for extraction and rectification. The extraction pressure was 155 by the valve 18.
It was set to kg / cm 2 G. The extraction phase obtained by extracting the fatty acid ethyl ester was depressurized to 30 kg / cm 2 G by the decompression valve 19 and the extract was separated in the separation tank 20. The carbon dioxide from which the extract had been separated was calibrated with a gas meter 21 and released outside the system. The amount of extract is on average 0.2 kg / hour,
EPA and DHA concentrations are 2-5% by weight, 1-
The range of 3% by weight was changed. On the other hand, when the unextracted substance was withdrawn from the lower part of the extraction tower at a flow rate of 0.4 kg / hour, E
The concentration of PA and DHA is 38 to 43% by weight, respectively.
And in the range of 24-28% by weight.
【００１１】[0011]
【表１】 [Table 1]
【００１２】実施例２ 抽出塔のヒータ１５を調整し、抽出塔の温度を上部より
順に、６０、５５、５０、４５、４０および３５℃とし
た点を除き、実施例１と同様の条件で抽出を行った。抽
出塔からは、平均０．３６ｋｇ／時で抽出物が得られ、
ＥＰＡおよびＤＨＡ濃度はそれぞれ、３３〜３８重量
％、４〜７重量％の範囲を変化した。また、抽出塔の下
部より未抽出物を０．２４ｋｇ／時の流量で抜き出し
た。ＥＰＡおよびＤＨＡ濃度はそれぞれ、１４〜１８重
量％および３５〜３９重量％であった。抽出塔の温度条
件を変えることによって、ＥＰＡが抽出相側に、またＤ
ＨＡが抽出残渣側に濃縮された。Example 2 Under the same conditions as in Example 1, except that the heater 15 of the extraction tower was adjusted so that the temperatures of the extraction tower were set to 60, 55, 50, 45, 40 and 35 ° C. in order from the top. Extraction was performed. An extract was obtained from the extraction tower at an average of 0.36 kg / hour,
The EPA and DHA concentrations varied in the range of 33-38 wt%, 4-7 wt%, respectively. Further, the unextracted substance was extracted from the lower part of the extraction tower at a flow rate of 0.24 kg / hour. The EPA and DHA concentrations were 14-18 wt% and 35-39 wt%, respectively. By changing the temperature condition of the extraction tower,
HA was concentrated on the extraction residue side.
【００１３】比較例１ 図２の装置を用いて、実施例１と同じ組成の脂肪酸エチ
ルエステル１０を１ｋｇ／時の流量で、直径３ｍｍ、長
さ３ｍｍのディクソンを充填した内径３０ｍｍ、高さ３
ｍの抽出塔１４に供給した。抽出塔の温度は、塔の外側
に設けた６個のヒータ１５によって調節し、上部より順
に７０、６６、６２、５８、５４、５０℃とし、下部は
５０℃とした。ボンベ２からポンプ３によって加圧し、
熱交換器４において二酸化炭素を流量１３．３ｋｇ／時
で抽出塔に供給し、抽出および精留を行った、抽出圧力
は、弁７によって、１５５ｋｇ／ｃｍ2Ｇ に設定した。
脂肪酸エチルエステルを抽出した抽出相は、減圧弁８で
３０ｋｇ／ｃｍ2Ｇ まで減圧し、分離槽９で抽出物を分
離した。抽出物を分離した二酸化炭素は、ガスメータ１
０で検量して系外に放出した。抽出物の量は、平均０．
２７ｋｇ／時であり、ＥＰＡおよびＤＨＡ濃度はそれぞ
れ３〜５重量％、１〜２重量％の範囲を変化した。抽出
塔の下部より未抽出物を０．７３ｋｇ／時の流量で抜き
出したところ、ＥＰＡおよびＤＨＡの濃度はそれぞれ、
２２〜２５重量％および１３〜１６重量％の範囲にあっ
た。Comparative Example 1 Using the apparatus shown in FIG. 2, fatty acid ethyl ester 10 having the same composition as in Example 1 was filled with Dickson having a diameter of 3 mm and a length of 3 mm at a flow rate of 1 kg / hour.
m to the extraction tower 14. The temperature of the extraction tower was adjusted by six heaters 15 provided on the outside of the tower, and was 70, 66, 62, 58, 54, 50 ° C. from the upper part, and 50 ° C. in the lower part. Pressurize from cylinder 2 with pump 3,
Carbon dioxide was supplied to the extraction tower in the heat exchanger 4 at a flow rate of 13.3 kg / hour for extraction and rectification. The extraction pressure was set to 155 kg / cm 2 G by the valve 7.
The extraction phase in which the fatty acid ethyl ester was extracted was decompressed to 30 kg / cm 2 G by the decompression valve 8, and the extract was separated in the separation tank 9. The carbon dioxide from which the extract has been separated is measured by the gas meter 1
It was calibrated at 0 and released outside the system. The amount of extract is on average 0.
It was 27 kg / hour, and the EPA and DHA concentrations varied in the range of 3 to 5% by weight and 1 to 2% by weight, respectively. When the unextracted substance was extracted from the lower part of the extraction tower at a flow rate of 0.73 kg / hour, the EPA and DHA concentrations were
It was in the range of 22-25% by weight and 13-16% by weight.
【００１４】[0014]
【発明の効果】超臨界状態もしくは亜臨界状態の流体に
よって、脂肪酸の低級アルコールエステルの混合物を抽
出し、抽出残渣を超臨界状態もしくは亜臨界状態の流体
によって精留機能を有する抽出塔において抽出したの
で、抽出と精留の両者の作用によって脂肪酸エステルの
混合物中からＥＰＡあるいはＤＨＡを濃縮分離すること
ができる。EFFECT OF THE INVENTION A mixture of a lower alcohol ester of a fatty acid is extracted with a fluid in a supercritical state or a subcritical state, and an extraction residue is extracted with a fluid in a rectification function by a fluid in the supercritical state or subcritical state. Therefore, EPA or DHA can be concentrated and separated from the mixture of fatty acid esters by the actions of both extraction and rectification.
【図１】本発明の抽出分離方法に使用する装置を説明す
る図である。FIG. 1 is a diagram illustrating an apparatus used in the extraction and separation method of the present invention.
【図２】比較例の抽出分離方法に使用する装置を説明す
る図である。FIG. 2 is a diagram illustrating an apparatus used in the extraction / separation method of the comparative example.
１…抽出槽、２…ボンベ、３…ポンプ、４…分離槽、５
…ガスメーター、６…弁、７…減圧弁、８…加熱装置、
９…熱交換器、１０…減圧弁、１１…抽出槽 １…抽出槽、２…ボンベ、３…ポンプ、４…熱交換器、
５…加温装置、６…脂肪酸エチルエステル、７…弁、８
…減圧弁、９…分離槽、１０…ガスメータ、１１…抽出
残渣、１２…ポンプ、１３…充填物ディクソン、１４…
抽出塔、１５…ヒータ、１６…ポンプ、１７…熱交換
器、１８…弁、１９…減圧弁、２０…分離槽、２１…ガ
スメータ1 ... Extraction tank, 2 ... Cylinder, 3 ... Pump, 4 ... Separation tank, 5
... Gas meter, 6 ... valve, 7 ... pressure reducing valve, 8 ... heating device,
9 ... Heat exchanger, 10 ... Pressure reducing valve, 11 ... Extraction tank 1 ... Extraction tank, 2 ... Cylinder, 3 ... Pump, 4 ... Heat exchanger,
5 ... Heating device, 6 ... Fatty acid ethyl ester, 7 ... Valve, 8
... Pressure reducing valve, 9 ... Separation tank, 10 ... Gas meter, 11 ... Extraction residue, 12 ... Pump, 13 ... Packing Dickson, 14 ...
Extraction tower, 15 ... Heater, 16 ... Pump, 17 ... Heat exchanger, 18 ... Valve, 19 ... Pressure reducing valve, 20 ... Separation tank, 21 ... Gas meter
Claims (2)
て、脂肪酸エステルの混合物を抽出槽において超臨界状
態もしくは亜臨界状態の状態の流体によって抽出分離し
た後に、抽出残渣を精留機能を有する抽出塔に導入し、
超臨界状態もしくは亜臨界状態の流体を供給して抽出分
離し、抽出相もしくは抽出残渣中に特定の脂肪酸エステ
ルを濃縮分離することを特徴とする脂肪酸エステルの濃
縮分離方法。1. A method for concentrating and separating a fatty acid ester, wherein a mixture of fatty acid esters is extracted and separated by a fluid in a supercritical state or a subcritical state in an extraction tank, and then the extraction residue is introduced into an extraction column having a rectification function. Then
A method for concentrating and separating a fatty acid ester, comprising supplying a fluid in a supercritical state or a subcritical state to perform extraction and separation, and concentrating and separating a specific fatty acid ester in an extraction phase or an extraction residue.
Ａ）又はドコサヘキサエン酸（ＤＨＡ）であり、抽出温
度が４６〜１００℃、抽出圧力が、８０〜３００気圧で
ある特許請求の範囲１項記載の方法。2. The fatty acid is eicosapentaenoic acid (EP
The method according to claim 1, which is A) or docosahexaenoic acid (DHA), the extraction temperature is 46 to 100 ° C., and the extraction pressure is 80 to 300 atm.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7203445A JPH0952866A (en) | 1995-08-09 | 1995-08-09 | Concentrated separation of fatty acid ester |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7203445A JPH0952866A (en) | 1995-08-09 | 1995-08-09 | Concentrated separation of fatty acid ester |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0952866A true JPH0952866A (en) | 1997-02-25 |
Family
ID=16474239
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7203445A Pending JPH0952866A (en) | 1995-08-09 | 1995-08-09 | Concentrated separation of fatty acid ester |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0952866A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1073867C (en) * | 1998-10-23 | 2001-10-31 | 潘见 | Separation method for material composition by supercritical fluid crystallization |
| CN103398887A (en) * | 2013-08-08 | 2013-11-20 | 上海天科化工检测有限公司 | Step-by-step liquefied composite type trace extraction device |
-
1995
- 1995-08-09 JP JP7203445A patent/JPH0952866A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN1073867C (en) * | 1998-10-23 | 2001-10-31 | 潘见 | Separation method for material composition by supercritical fluid crystallization |
| CN103398887A (en) * | 2013-08-08 | 2013-11-20 | 上海天科化工检测有限公司 | Step-by-step liquefied composite type trace extraction device |
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