EP0255824A1 - Un procédé de fabrication de concentré d'huile de poisson raffinée. - Google Patents

Un procédé de fabrication de concentré d'huile de poisson raffinée.

Info

Publication number
EP0255824A1
EP0255824A1 EP86906964A EP86906964A EP0255824A1 EP 0255824 A1 EP0255824 A1 EP 0255824A1 EP 86906964 A EP86906964 A EP 86906964A EP 86906964 A EP86906964 A EP 86906964A EP 0255824 A1 EP0255824 A1 EP 0255824A1
Authority
EP
European Patent Office
Prior art keywords
fatty acid
fish oil
concentrate
urea
cholesterol
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.)
Granted
Application number
EP86906964A
Other languages
German (de)
English (en)
Other versions
EP0255824B1 (fr
Inventor
Harald Breivik
Bernt Borretzen
Tore-Erling Jorgensen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Norsk Hydro ASA
Original Assignee
Norsk Hydro ASA
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Norsk Hydro ASA filed Critical Norsk Hydro ASA
Priority to AT86906964T priority Critical patent/ATE49774T1/de
Publication of EP0255824A1 publication Critical patent/EP0255824A1/fr
Application granted granted Critical
Publication of EP0255824B1 publication Critical patent/EP0255824B1/fr
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

Links

Classifications

    • 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
    • C11B3/00—Refining fats or fatty oils
    • C11B3/001—Refining fats or fatty oils by a combination of two or more of the means hereafter

Definitions

  • a refined fish oil concentrate and the production process for same A refined fish oil concentrate and the production process for same.
  • the present invention concerns a refined fish oil concentrate as well as the production process for same.
  • cholesterol and useful biproducts such as urea adducts of fatty acid compounds are produced, in addition to higher unsaturated fatty acids.
  • waste products from the fish refining indu ⁇ stry contain usable products, among others fatty acids, chol ⁇ esterol, proteins and enzymes. These are either fat-soluble or water-soluble. Such waste products are normally referred to as fish entrails.
  • the water-soluble portion containing proteins and enzymes may be separated from the fat-soluble portion.
  • the present invention concerns only the fat-soluble portion of the waste products, but it can also be used for other refined fish oils such as occur for instance in the fish product industry. In the following this will be called fish oil product.
  • fatty acids the following may be specified as suitable for the medicinal purpose referred to: eicosapentaenoic acid (EPA) and docosahexaenoic acid (DHA). Both fatty acids are « ⁇ > 3-fatty acids of the C-20 and C-22 acids. Their nomenclature according to the IUPAC system is:
  • EDA eicosapentaensoic acid
  • DHA docosahexaenoic acid
  • 20 and 22 indicate the number of C-atoms in the mole ⁇ cule of fatty acid, 5 and 6 the number of unsaturated bondings, and ⁇ 3 that the last unsaturated bonding is posi ⁇ tioned in a distance of 3 carbon atoms from the u)-position.
  • the fat soluble portion of cod entrails usually contains 10 - 25% of the essential fatty acid compounds EPA and DHA, as well as 2 - 4% cholesterol.
  • the remainder is mainly fatty acid compounds with lower unsaturation, such as pure fatty acids or their glycerides.
  • the purpose of the invention is to separate the essential fatty acid compounds from cholesterol and the remaining fatty acid compounds.
  • Another purpose of the invention is to produce from a non-uniform raw material containing marine fatty acids and/or esters of these fatty acids, as well as cholesterol as main components after trans-esterification with a lower alcohol, and under alkaline conditions produce a concentrate con ⁇ taining the essential u3-fatty acid compounds, EPA and DHA, as well as isolate the cholesterol and the urea adduct of the saturated and lower unsaturated fatty acid compounds, which then appear in their own product fractions.
  • esters for instance as methyl or ethyl esters.
  • trans-esterification and esterification for instance with methanol for production of fatty acid methyl esters.
  • This basic material is well suited for further separation of essential fatty acid compounds and cholesterol from the remaining less important fatty acid compounds.
  • Another patent, SU 950.393 describes a method for production of cholesterol from for instance fish waste products by hydrolysing the fatty acid compounds and converting, them to soaps. These are then subjected to an extraction of trichlor- ethylene at room temperature, whereby the cholesterol is com ⁇ bined with the trichlorethylene and this compound is then subject to further separation.
  • GB 1.240.513 also concerns a separation technique by means of urea where the raw material consists of pure methyl and ethyl esters of the C,g-C,gfatty acids. Urea precipitation occurs in a neutral environment with a surplus of the rele ⁇ vant alcohol. The purpose is to be able to obtain a stronger concentration of the V -linolenic acid.
  • the above-mentioned fatty acid esters do not contain any higher fatty acids other than C-18 in the form of stearic acid, oleic acid, linoleic acid and linolenic acid, which after the urea precipitation and. separation of the urea adduct from the rest of the material has obtained a higher content of X -linolenic acid by means chromotography.
  • the higher unsaturated fatty acid compounds 20:5 u)3 and 22:6 -J3 may be concentrated according to a method described in J 59-071396 where the fatty acid compounds men ⁇ tioned are extracted by means of polar solvents, such as ace ⁇ tone, methyl ethyl ketone, methanol, ethanol, and similar solvents, whereby a soluble and an insoluble extract are formed. Thereafter the extract is further processed to obtain essential fatty acid compounds.
  • polar solvents such as ace ⁇ tone, methyl ethyl ketone, methanol, ethanol, and similar solvents
  • Another special feature is that the precipitation of urea takes place in an alkaline environment, and in such a way that the alkaline environment is created through applying the base only in catalytic quantities such as a catalytic agent for the trans-esterification of glycerides to methyl esters and not as a means of saponification of the fatty acids.
  • a third special feature is that the trans-esterification takes place at room temperature.
  • a result of trans-esterification at low temperature and in an environment with low alkalinity is that isomerization of the double compounds is avoided, which results in a more uniform product with no toxic effect.
  • transcon- figurations are avoided.
  • the remaining solution is thereafter extracted by means of non-polar solvents, among others hex ⁇ ane, whereby the t ⁇ 3-fatty acids as well as cholesterol will be found in the hexane phase.
  • the basic material is fat and/or fatty acids from fish and especially fat and/or fatty acids obtained from the fish processing industry in connection with ensilage and or auto- catalysis processes, but the process may also be used for other forms of marine fat.
  • This fatty raw material is called a fish oil product in the claims.
  • Such fat/fatty acids have a high content of saturated, unsaturated and polyunsaturated fatty acids with a chain length C 18, C 20 and C 22 as well as a certain amount of cholesterol, vitamins and other fat soluble products which are undefinable, usually characterized as unsaponifiable, as well as fatty acid compounds with shorter chain lengths.
  • B alcohol with a low boiling point
  • B for instance methanol or ethanol, prefer ⁇ ably methanol
  • C auxiliary compounds
  • Potassium hydroxide may be used as a catalytic agent and in order to prevent oxidization, especially when heavy metals are present, such as chromium, iron, cobalt, nickel and copper, small amounts of the sodium salt of ethyl- enediaminetetra-acetic acid (EDTA-Na 3 ) may be added.
  • EDTA-Na 3 sodium salt of ethyl- enediaminetetra-acetic acid
  • the esterification and trans-esterification take place under moderate conditions and stirring at about 20° C for some hours.
  • the formation of alkyl esters is nearly complete when the ester product has changed its appearance from opalescent to clear.
  • the clear solution (Dl) therefore contains alkyl esters of the fatty acids, glycerol, alkanol, as well as some water from the esterification of the free fatty acids.
  • urea (E) and alkanol (B) are added and stirred in until everything is completely dissolved.
  • the amount of urea depends on the composition of the fatty acids so that if the raw material (A) contains 6-8% EPA by weight, urea is added in the ratio 3 parts urea by weight to 1 part alkyl ester. In order to ensure that the components are completely soluble, 9 parts alkanol by weight is added.
  • the slightly alkaline filter mass (G) is saturated with hex ⁇ ane and is extracted by means of this solvent through a known technique as for instance by a continuing fluid-to-fluid counter current process, whereafter a further quantity of adduct of urea fatty ester may be crystallized.
  • two fluids are formed, consisting of hexane (I) and a residue (K). Box 4.
  • the hexane extract (I) which contains the alkyl-fatty esters of the polyunsaturated fatty acids 18:4 ⁇ )3, 20:5 tt>3-and 22:64)3 as well as cholesterol as the most important com ⁇ ponents, is washed in a diluted hydrochloric acid ( ) in order to neutralize possible potassium soaps of the essential polyunsaturated fatty acids in the hexane extract.
  • the washing water is decanted.
  • Hexane (H) is thereafter removed by evaporation of the extract (I) so that a concentrate is produced which is free from solvents (N) and which contains the compounds that are essential for the invention, the fatty acid compounds EPA and DHA as well as cholesterol.
  • the dehydrated extract normally contains 20-30 % EPA, 35-45% DHA, 10-20% other polyunsaturated fatty acids, as well as 5-15% cholesterol and undefined compounds, all by weight, but the composition referred to will depend on the type of fish used, the time of year the fish is caught, and the type and condition of the raw material.
  • the concentrate of alkyl fatty acid ester (N) is thereafter cooled to approx. minus 25° C, whereafter cholesterol (0) is crystallized. This is centrifuged/filtered. Further impurities which are present in the concentrate (N) may be removed by cooling the mixture to a temperature of lower than minus 25 C, whereafter certain undefined com ⁇ pounds are precipitated and filtered by means of a known method.
  • the remaining «J3-concentrate (P) thus contains 20-35% EPA, 35-50% DHA and 15-25% of other polyunsaturated ⁇ 3-fatty acid compounds (all by weight) as well as unsatur ⁇ ated fatty acid compounds which are not essential for the invention.
  • Product (P) which contains the alkyl esters of the corre ⁇ sponding ⁇ 3-fatty acids may be utilized as it is or the con ⁇ centration of EPA and DHA may be increased.
  • the product contains only small amounts of other fatty acids with the same chain length as EPA and DHA, it is well suited for separation of the essential fatty acids, EPA and DHA by means of supercritical fluid extraction.
  • Another method for increasing the concentration is by means of preparative liquid chromatography by which method a mors than 90% purity of the essential fatty acids is obtained.
  • the hexane fractions (R) contain free fatty acids as well as some of their alkyl esters and fairly high percentages of EPA and DHA, but also a fairly substantial portion of C 18-, C 20- and C 22-fatty acids with lower unsaturation.
  • This acid solution contains water, alcohol, alkanol, glycerol, urea and other products which may be retrieved by a separate process which is not described here.
  • the fatty acid components of the hexane fraction are increased by evaporating hexane (H) in a separate piece of equipment.
  • the remaining solution is esterified using lower alkanols, for instance methanol or ethanol by means of an appropriate catalytic agent (V) which for instance may be dehydrated hydrochloric acid, acetic acid chloride or boron-trichloride.
  • V catalytic agent
  • the resultant alkyl ester (D2) from the fatty acid components (T) from box 7 may be processed in various ways, for instance returned to box 2 for urea precipitation of the less unsatur ⁇ ated fatty acids.
  • the whole mixture was subjected to stirring for 15 hours at 20°C in order to bring about a trans-esterification of the glycerides to methyl esters and esterification of the free fatty acids to methyl esters.
  • the urea adduct was separated from the solution by decanting and filtering according to an ordinary, known technique. Result: 100.1 kg urea adduct (F). Thereafter the solution was cooled to 0 - 4° C, whereby an additional 5.1 kg urea adduct (F) could be filtrated from the solution.
  • This filtrate (G) contained u/3-polyunsaturated fatty acid methyl esters, cholesterol and a residue of unwanted fatty acid fractions with lower unsaturated C 18, C 20 and C 22 fatty acid methyl esters.
  • To this filtrate we added hexane for saturation, whereby a further amount of urea adduct (22 kg) could be separated.
  • This hexane-saturated solution was extracted in a counter-current with hexane so that the hexane extract (I) finally made up approx. 300 1. The remaining unextracted solution is called (K). The hexane extract was thereafter evaporated.
  • the yield of 3-fatty acid methyl ester concentrate 10.2 kilos.
  • the concentrate (N) which contained 23% EPA , 41% DHA and 8% cholesterol, all by weight, was thereafter cooled to minus 25°C, whereby pure cholesterol (0) crystallized and was removed by means of centrifuging during which time the resi ⁇ due in the centrifuge was washed with hexane with a lower temperature in order to remove the fatty acid methyl esters from the cholesterol crystals. Yield: 760 g pure cholesterol.
  • the concentrated filtrate (P) contained 25% EPA-methylester, 43% DHA-methylester by weight based on the fatty acid portion and traces of cholesterol.
  • Another advantage with the invention is that it is possible to produce a urea adduct based on the same procedure where a trans-esterification has been done from glycerides to alkanol esters without following the cumbersome procedure by first producing the fatty acids, esterify these with alkanol and then separate them by means of the fractionated urea preci ⁇ pitation.

Landscapes

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

Abstract

Raffinage d'un produit à base de déchets de poisson de manière à former un concentré d'un ester d'alkyle de omega3-acide gras avec 20 à 30% d'un ester d'alkyle d'acide eicosapentaenoïque et 35 à 50% d'un ester d'alkyle d'acide docosahexaénoïque (les deux en poids) dépourvu de cholestérol. Le omega3-concentré est produit par précipitation avec de l'urée des esters des non-omega3-acide gras de manière à permettre l'extraction du filtrat provenant de la précipitation à l'aide d'hexane pour la transmission des esters de omega3-acide gras et du cholestérol à l'extrait d'hexane. L'hexane est ensuite éliminé. Le concentré restant d'ester d'acide gras avec le cholestérol est refroidi jusqu'à une température non inférieure à -50oC, le cholestérol étant ainsi cristallisé. Le reste est un omega3-concentré présentant la composition précitée.
EP86906964A 1985-12-19 1986-11-21 Un procédé de fabrication de concentré d'huile de poisson raffinée Expired - Lifetime EP0255824B1 (fr)

Priority Applications (1)

Application Number Priority Date Filing Date Title
AT86906964T ATE49774T1 (de) 1985-12-19 1986-11-21 Ein verfahren zur herstellung von raffiniertem fischoelkonzentrat.

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
NO855147 1985-12-19
NO855147A NO157302C (no) 1985-12-19 1985-12-19 Fremgangsmaate for fremstilling av et fiskeoljekonsentrat.

Publications (2)

Publication Number Publication Date
EP0255824A1 true EP0255824A1 (fr) 1988-02-17
EP0255824B1 EP0255824B1 (fr) 1990-01-24

Family

ID=19888637

Family Applications (1)

Application Number Title Priority Date Filing Date
EP86906964A Expired - Lifetime EP0255824B1 (fr) 1985-12-19 1986-11-21 Un procédé de fabrication de concentré d'huile de poisson raffinée

Country Status (15)

Country Link
EP (1) EP0255824B1 (fr)
AR (1) AR242111A1 (fr)
AU (1) AU6621186A (fr)
CA (1) CA1303416C (fr)
DD (1) DD261805A1 (fr)
DE (1) DE3668467D1 (fr)
IE (1) IE59171B1 (fr)
IS (1) IS1425B6 (fr)
MA (1) MA20840A1 (fr)
MX (1) MX168698B (fr)
NO (1) NO157302C (fr)
NZ (1) NZ218500A (fr)
PT (1) PT83991B (fr)
WO (1) WO1987003899A1 (fr)
ZA (1) ZA868927B (fr)

Cited By (12)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US6395778B1 (en) 2000-01-11 2002-05-28 Omegatech, Inc. Process for making an enriched mixture of polyunsaturated fatty acid esters
WO2005049772A1 (fr) * 2003-11-19 2005-06-02 Pro Aparts-Investimentos E Consultoria Lda Procede de preparation d'une composition comprenant des composes insatures
US7462643B1 (en) 1999-02-17 2008-12-09 Pfizer Italia S.R.L. Essential fatty acids in the prevention of cardiovascular events
US9150816B2 (en) 2013-12-11 2015-10-06 Novasep Process Sas Chromatographic method for the production of polyunsaturated fatty acids
US9347020B2 (en) 2011-07-06 2016-05-24 Basf Pharma Callanish Limited Heated chromatographic separation process
US9428711B2 (en) 2013-05-07 2016-08-30 Groupe Novasep Chromatographic process for the production of highly purified polyunsaturated fatty acids
WO2016182452A1 (fr) 2015-05-13 2016-11-17 Epax Norway As Acides gras polyinsaturés à chaîne très longue
US9695382B2 (en) 2011-07-06 2017-07-04 Basf Pharma (Callanish) Limited SMB process for producing highly pure EPA from fish oil
US9694302B2 (en) 2013-01-09 2017-07-04 Basf Pharma (Callanish) Limited Multi-step separation process
US9790162B2 (en) 2009-12-30 2017-10-17 Basf Pharma (Callanish) Limited Simulated moving bed chromatographic separation process
US10975031B2 (en) 2014-01-07 2021-04-13 Novasep Process Method for purifying aromatic amino acids
US11718640B2 (en) 2017-09-14 2023-08-08 Fermenta Biotech Limited Process for extraction of cholesterol from fish oil waste residue

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GB8819110D0 (en) * 1988-08-11 1988-09-14 Norsk Hydro As Antihypertensive drug & method for production
US5336792A (en) * 1990-03-12 1994-08-09 Einar Sola Process for enrichment of fat with regard to polyunsaturated fatty acids and phospholipids, and application of such enriched fat
SE9303446D0 (sv) * 1993-10-20 1993-10-20 Trikonex Ab A novel urea fractionation process
GB9404483D0 (en) * 1994-03-08 1994-04-20 Norsk Hydro As Refining marine oil compositions
TW425285B (en) 1996-06-10 2001-03-11 Viva America Marketing Inc Fish oil and garlic nutritive supplement
US6313167B1 (en) 1997-06-16 2001-11-06 Nippon Suisan Kaisha Ltd. Composition having capability of removing risk factor during exercise
NO309795B1 (no) * 1998-07-01 2001-04-02 Norsk Hydro As FremgangsmOte for O stabilisere oljer samt anvendelse derav, fremgangsmOte for O stabilisere pigmenter, og fremgangsmOte for fremstilling av for
NO311041B1 (no) * 1999-12-22 2001-10-01 Norsk Hydro As Stabilisering av pigmenter og flerumettede oljer og oljekonsentrater
AT414205B (de) 2000-06-20 2006-10-15 Vis Vitalis Lizenz & Handels Verfahren zur herstellung von ungesättigtem fettsäure-trockenkonzentrat
ITMI20010129A1 (it) 2001-01-25 2002-07-25 Pharmacia & Upjohn Spa Acidi grassi essenziali nella terapia di insufficienza cardiaca e scompenso cardiaco
SE0202188D0 (sv) 2002-07-11 2002-07-11 Pronova Biocare As A process for decreasing environmental pollutants in an oil or a fat, a volatile fat or oil environmental pollutants decreasing working fluid, a health supplement, and an animal feed product
EP2295529B2 (fr) 2002-07-11 2022-05-18 Basf As Procédé de diminution des polluants environnementaux dans une huile ou une graisse et produit d'alimentation pour poissons
DK2447356T3 (en) 2005-06-07 2016-06-06 Dsm Nutritional Products Ag Eukaryotic MICROORGANISMS FOR PRODUCTION OF LIPIDS AND ANTIOXIDANTS
ITMI20051560A1 (it) * 2005-08-10 2007-02-11 Tiberio Bruzzese Composizione di acidi grassi n-3 con elevata concentrazione di epa e-o dha e contenente acidi grassi n-6
WO2008129358A2 (fr) 2006-08-01 2008-10-30 Ocean Nutrition Canada Ltd. Microbes produisant des huiles et procedes de modification associes
ITMI20102297A1 (it) 2010-12-15 2012-06-16 Prime Europ Therapeuticals Procedimento per stabilizzare acidi grassi poliinsaturi per mezzo di idruri metallici
US8889895B2 (en) * 2011-03-08 2014-11-18 Cognis Ip Management Gmbh Process for the distillation of fatty acid esters
GB201111589D0 (en) 2011-07-06 2011-08-24 Equateq Ltd New modified process
GB201111591D0 (en) 2011-07-06 2011-08-24 Equateq Ltd Further new process
GB201111601D0 (en) 2011-07-06 2011-08-24 Equateq Ltd New process
EP2970926B1 (fr) 2013-03-13 2018-01-31 DSM Nutritional Products AG Modification génétique de micro-organismes
US9163198B2 (en) * 2014-01-17 2015-10-20 Orochem Technologies, Inc. Process for purification of EPA (eicosapentanoic acid) ethyl ester from fish oil
WO2016028235A1 (fr) * 2014-08-18 2016-02-25 Chiang Mai University Système et procédé d'extraction et/ou de concentration
CN107666904B (zh) 2015-03-26 2022-02-01 提贝托·布鲁泽塞 多不饱和脂肪酸的纯化组合物、其制备方法及其用途
AR104042A1 (es) 2015-03-26 2017-06-21 Mara Renewables Corp Producción de alta densidad de biomasa y aceite utilizando glicerol en bruto
AU2016293487B2 (en) 2015-07-13 2021-07-01 MARA Renewables Corporation Enhancing microalgal metabolism of xylose
US10851395B2 (en) 2016-06-10 2020-12-01 MARA Renewables Corporation Method of making lipids with improved cold flow properties
US10196586B1 (en) * 2018-02-14 2019-02-05 Golden Omega S.A. Feed ingredient

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IT1176916B (it) * 1984-10-10 1987-08-18 Elvira Pistolesi Composizione farmaceutica o dietetica ad elevata attivita' antitrombotica e antiarteriosclerotica

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See references of WO8703899A1 *

Cited By (17)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US7462643B1 (en) 1999-02-17 2008-12-09 Pfizer Italia S.R.L. Essential fatty acids in the prevention of cardiovascular events
US6395778B1 (en) 2000-01-11 2002-05-28 Omegatech, Inc. Process for making an enriched mixture of polyunsaturated fatty acid esters
WO2005049772A1 (fr) * 2003-11-19 2005-06-02 Pro Aparts-Investimentos E Consultoria Lda Procede de preparation d'une composition comprenant des composes insatures
US7541480B2 (en) 2003-11-19 2009-06-02 Pro Aparts-Investimentos E Consultoria Lda Process for the preparation of a composition comprising unsaturated compounds
US9790162B2 (en) 2009-12-30 2017-10-17 Basf Pharma (Callanish) Limited Simulated moving bed chromatographic separation process
US9695382B2 (en) 2011-07-06 2017-07-04 Basf Pharma (Callanish) Limited SMB process for producing highly pure EPA from fish oil
US9347020B2 (en) 2011-07-06 2016-05-24 Basf Pharma Callanish Limited Heated chromatographic separation process
US9771542B2 (en) 2011-07-06 2017-09-26 Basf Pharma Callanish Ltd. Heated chromatographic separation process
US10179759B2 (en) 2013-01-09 2019-01-15 Basf Pharma (Callanish) Limited Multi-step separation process
US9694302B2 (en) 2013-01-09 2017-07-04 Basf Pharma (Callanish) Limited Multi-step separation process
US10214475B2 (en) 2013-01-09 2019-02-26 Basf Pharma (Callanish) Limited Multi-step separation process
US10723973B2 (en) 2013-01-09 2020-07-28 Basf Pharma (Callanish) Limited Multi-step separation process
US9428711B2 (en) 2013-05-07 2016-08-30 Groupe Novasep Chromatographic process for the production of highly purified polyunsaturated fatty acids
US9150816B2 (en) 2013-12-11 2015-10-06 Novasep Process Sas Chromatographic method for the production of polyunsaturated fatty acids
US10975031B2 (en) 2014-01-07 2021-04-13 Novasep Process Method for purifying aromatic amino acids
WO2016182452A1 (fr) 2015-05-13 2016-11-17 Epax Norway As Acides gras polyinsaturés à chaîne très longue
US11718640B2 (en) 2017-09-14 2023-08-08 Fermenta Biotech Limited Process for extraction of cholesterol from fish oil waste residue

Also Published As

Publication number Publication date
ZA868927B (en) 1987-08-26
AR242111A1 (es) 1993-03-31
NO855147L (no) 1987-06-22
NZ218500A (en) 1989-03-29
IE59171B1 (en) 1994-01-12
IS3159A7 (is) 1987-06-20
MA20840A1 (fr) 1987-07-01
NO157302C (no) 1988-02-24
PT83991A (en) 1987-01-01
PT83991B (pt) 1989-01-17
EP0255824B1 (fr) 1990-01-24
IE863064L (en) 1987-06-19
WO1987003899A1 (fr) 1987-07-02
AU6621186A (en) 1987-07-15
DE3668467D1 (de) 1990-03-01
NO157302B (no) 1987-11-16
DD261805A1 (de) 1988-11-09
IS1425B6 (is) 1990-03-28
MX168698B (es) 1993-06-04
CA1303416C (fr) 1992-06-16

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