EP2838630A2 - Verfahren zum raffinieren von squalen aus mikroalgen - Google Patents

Verfahren zum raffinieren von squalen aus mikroalgen

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Publication number
EP2838630A2
EP2838630A2 EP13720486.3A EP13720486A EP2838630A2 EP 2838630 A2 EP2838630 A2 EP 2838630A2 EP 13720486 A EP13720486 A EP 13720486A EP 2838630 A2 EP2838630 A2 EP 2838630A2
Authority
EP
European Patent Office
Prior art keywords
squalene
extract
weight
biomass
composition
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
Application number
EP13720486.3A
Other languages
English (en)
French (fr)
Inventor
Philippe Looten
Samuel PATINIER
Michel Perrut
Vincent Perrut
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.)
Roquette Freres SA
Original Assignee
Roquette Freres SA
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
Priority claimed from FR1253496A external-priority patent/FR2989373B1/fr
Application filed by Roquette Freres SA filed Critical Roquette Freres SA
Publication of EP2838630A2 publication Critical patent/EP2838630A2/de
Pending legal-status Critical Current

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    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/02—Preparation of hydrocarbons or halogenated hydrocarbons acyclic
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L17/00—Food-from-the-sea products; Fish products; Fish meal; Fish-egg substitutes; Preparation or treatment thereof
    • A23L17/60—Edible seaweed
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23L—FOODS, FOODSTUFFS, OR NON-ALCOHOLIC BEVERAGES, NOT COVERED BY SUBCLASSES A21D OR A23B-A23J; THEIR PREPARATION OR TREATMENT, e.g. COOKING, MODIFICATION OF NUTRITIVE QUALITIES, PHYSICAL TREATMENT; PRESERVATION OF FOODS OR FOODSTUFFS, IN GENERAL
    • A23L33/00—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof
    • A23L33/10—Modifying nutritive qualities of foods; Dietetic products; Preparation or treatment thereof using additives
    • A23L33/105—Plant extracts, their artificial duplicates or their derivatives
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K31/00—Medicinal preparations containing organic active ingredients
    • A61K31/01—Hydrocarbons
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K36/00—Medicinal preparations of undetermined constitution containing material from algae, lichens, fungi or plants, or derivatives thereof, e.g. traditional herbal medicines
    • A61K36/02—Algae
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K8/00—Cosmetics or similar toiletry preparations
    • A61K8/18—Cosmetics or similar toiletry preparations characterised by the composition
    • A61K8/30—Cosmetics or similar toiletry preparations characterised by the composition containing organic compounds
    • A61K8/31—Hydrocarbons
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K8/00—Cosmetics or similar toiletry preparations
    • A61K8/18—Cosmetics or similar toiletry preparations characterised by the composition
    • A61K8/96—Cosmetics or similar toiletry preparations characterised by the composition containing materials, or derivatives thereof of undetermined constitution
    • A61K8/97—Cosmetics or similar toiletry preparations characterised by the composition containing materials, or derivatives thereof of undetermined constitution from algae, fungi, lichens or plants; from derivatives thereof
    • A61K8/9706—Algae
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K8/00—Cosmetics or similar toiletry preparations
    • A61K8/18—Cosmetics or similar toiletry preparations characterised by the composition
    • A61K8/96—Cosmetics or similar toiletry preparations characterised by the composition containing materials, or derivatives thereof of undetermined constitution
    • A61K8/97—Cosmetics or similar toiletry preparations characterised by the composition containing materials, or derivatives thereof of undetermined constitution from algae, fungi, lichens or plants; from derivatives thereof
    • A61K8/9706—Algae
    • A61K8/9711—Phaeophycota or Phaeophyta [brown algae], e.g. Fucus
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61P—SPECIFIC THERAPEUTIC ACTIVITY OF CHEMICAL COMPOUNDS OR MEDICINAL PREPARATIONS
    • A61P39/00—General protective or antinoxious agents
    • A61P39/06—Free radical scavengers or antioxidants
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61Q—SPECIFIC USE OF COSMETICS OR SIMILAR TOILETRY PREPARATIONS
    • A61Q19/00—Preparations for care of the skin
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0403—Solvent extraction of solutions which are liquid with a supercritical fluid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D11/00—Solvent extraction
    • B01D11/04—Solvent extraction of solutions which are liquid
    • B01D11/0426—Counter-current multistage extraction towers in a vertical or sloping position
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/34—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping with one or more auxiliary substances
    • B01D3/40—Extractive distillation
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C5/00—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms
    • C07C5/02—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation
    • C07C5/03—Preparation of hydrocarbons from hydrocarbons containing the same number of carbon atoms by hydrogenation of non-aromatic carbon-to-carbon double bonds
    • C—CHEMISTRY; METALLURGY
    • C07—ORGANIC CHEMISTRY
    • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
    • C07C7/00—Purification; Separation; Use of additives
    • C07C7/04—Purification; Separation; Use of additives by distillation
    • C07C7/05—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds
    • C07C7/08—Purification; Separation; Use of additives by distillation with the aid of auxiliary compounds by extractive distillation
    • 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
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/10—Production of fats or fatty oils from raw materials by extracting
    • C11B1/104—Production of fats or fatty oils from raw materials by extracting using super critical gases or vapours
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
    • C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
    • C12N1/12—Unicellular algae; Culture media therefor
    • C—CHEMISTRY; METALLURGY
    • C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
    • C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
    • C12P5/00—Preparation of hydrocarbons or halogenated hydrocarbons
    • C12P5/007—Preparation of hydrocarbons or halogenated hydrocarbons containing one or more isoprene units, i.e. terpenes
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K2236/00—Isolation or extraction methods of medicinal preparations of undetermined constitution containing material from algae, lichens, fungi or plants, or derivatives thereof, e.g. traditional herbal medicine
    • A61K2236/10—Preparation or pretreatment of starting material
    • A61K2236/19—Preparation or pretreatment of starting material involving fermentation using yeast, bacteria or both; enzymatic treatment
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K2236/00—Isolation or extraction methods of medicinal preparations of undetermined constitution containing material from algae, lichens, fungi or plants, or derivatives thereof, e.g. traditional herbal medicine
    • A61K2236/30—Extraction of the material
    • A61K2236/37—Extraction at elevated pressure or temperature, e.g. pressurized solvent extraction [PSE], supercritical carbon dioxide extraction or subcritical water extraction
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K2800/00—Properties of cosmetic compositions or active ingredients thereof or formulation aids used therein and process related aspects
    • A61K2800/10—General cosmetic use
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K2800/00—Properties of cosmetic compositions or active ingredients thereof or formulation aids used therein and process related aspects
    • A61K2800/80—Process related aspects concerning the preparation of the cosmetic composition or the storage or application thereof
    • A61K2800/85—Products or compounds obtained by fermentation, e.g. yoghurt, beer, wine
    • A—HUMAN NECESSITIES
    • A61—MEDICAL OR VETERINARY SCIENCE; HYGIENE
    • A61K—PREPARATIONS FOR MEDICAL, DENTAL OR TOILETRY PURPOSES
    • A61K2800/00—Properties of cosmetic compositions or active ingredients thereof or formulation aids used therein and process related aspects
    • A61K2800/80—Process related aspects concerning the preparation of the cosmetic composition or the storage or application thereof
    • A61K2800/86—Products or compounds obtained by genetic engineering
    • 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
    • Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
    • Y02E50/00—Technologies for the production of fuel of non-fossil origin
    • Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
    • 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

Definitions

  • the present invention relates to a process for refining squalene produced by fermentation from microorganisms, more particularly microalgae, more particularly those from the family of Thraustochytriales sp.
  • microalgae of the family Thraustochytriales sp Microalgae belonging to the species Schizochytrium sp. , Aurantiochytrium sp. and Thraustochytrium sp.
  • Squalene is a lipid present in all higher organisms, and is the common precursor of steroid hormones, both animal and vegetable, and some vitamins, such as vitamin D.
  • This unsaturated linear hydrocarbon is an isoprenoid with thirty carbon atoms and fifty hydrogen atoms, of formula: 2,6,10,15,19,23 - Hexamethyl
  • terpenes formed from isopentyl pyrophosphate which couples with dimethylallyl pyrophosphate to successively deliver geranyl and then farnesyl pyrophosphates, two molecules of which condense after reduction by NADPH to form squalene. under the action of squalene synthase.
  • this pathway coexists with other metabolic pathways leading to phytoene, precursor of chlorophyll, carotenoid pigments and terpenes in latex.
  • Squalene like its epoxy derivative on the terminal double bond, has the property of being transformed, thanks to specialized enzymes (cyclases), and remarkably regio- and stereoselectively, into triterpenes.
  • polycyclic of a great structural variety hopene and diplopterol in eukaryotes and tetrahymanol in protozoa (pentacyclic triperpenes); lanosterol in yeasts, fungi and mammals and cycloartol in plants (tetracyclic triperpenes).
  • Squalene has long been used, especially in Japan, as a dietary supplement.
  • adjuvants squalene or aluminum salts (used since 1926), is currently required for some vaccines that, inactivated or subunit, do not contain the signals allowing the immune system to implement the defense mechanisms appropriate.
  • Squalene avoids the need for repeated injections to ensure good protection. These uses of squalene reinforce the determination of those skilled in the art to have secure processes for producing high purity squalene.
  • this quality can open other routes of application in the medical field.
  • Squalene is classically extracted from shark liver from the depths.
  • liver accumulates many toxic compounds, such as heavy metals (including mercury) and other fat-soluble toxins.
  • the purity level of squalene is essential when used in the medical field, especially as adjuvants to vaccines.
  • first methods of producing squalene have been proposed from microorganisms, more particularly from natural yeasts or recombinant yeasts, in particular of the Saccharomyces type.
  • Saccharomyces cerevisiae is known for its ability to produce squalene, however in a very small amount: on the order of 0.041 mg / g of biomass (BHATTACHARJEE, P. et al, 2001, in World J. Microb. Biotechnol., 17, pp. 811-816).
  • the genes involved in the biosynthesis of squalene are multiple: including mevalonate kinase, phosphomevalonate kinase, pyrophosphomevalonate decarboxylase, isopentenyl pyrophosphate isomerase, HMGR (3-hydroxy-3-methylglutaryl-CoA reductase), and squalene synthetase.
  • the genes encoding many enzymes involved in the conversion of squalene to ergosterol including squalene epoxidase (ERG1), lanosterol synthetase, C14-dimethylase, dl4-reductase, C4-methyloxidase, C4 decarboxylase (ERG26), 3-ketoreductase, C24-methyltransferase, C8-isomerase, C5-desaturase, d22-desaturase and d24-reductase.
  • ESG1 squalene epoxidase
  • lanosterol synthetase C14-dimethylase
  • dl4-reductase C4-methyloxidase
  • C4 decarboxylase C4 decarboxylase
  • 3-ketoreductase C24-methyltransferase
  • C8-isomerase C5-
  • LEU2 [beta] -isopropylmalate dehydrogenase
  • oxidosqualene cyclase oxidosqualene cyclase
  • zymosterol-24-methyltransferase zymosterol-24-methyltransferase
  • ergosta-7 ergosta-7, 24 (28) -trienol-22-dehydrogenase.
  • Thraustochytriales including the genera Thraustochytrium, Aurantiochytrium and Schizochytrium), more particularly Schizochytrium mangrovei. or Schizochytrium limacinum.
  • microalgae also produce squalene in heterotrophic conditions (absence of light, supply of glucose as a carbon source), and can therefore be easily handled by those skilled in the field of fermentation of microorganisms.
  • squalene is the co-product of other lipid compounds of interest, such as docosahexaenoic acid (or DHA), a polyunsaturated fatty acid of the family G) 3.
  • DHA docosahexaenoic acid
  • squalene is mainly described as one of the components of the unsaponifiable fraction of commercial DHA oils (in addition to carotenoids and sterols).
  • the Schizochytrium mangrove FBI strain produces DHA at a rate of 6.2% by dry weight of cells, for 0.017% of squalene.
  • the plaintiff company has also helped to further improve the production of squalene by microalgae of the family Thraustochytriales sp. proposing a process for producing squalene at a level never before achieved in the field literature, ie at least 8 g of squalene per 100 g of biomass (in its French patent applications under examination).
  • supercritical fluid such as supercritical CO 2
  • the treated vegetable oil is avocado or soybean oil.
  • the third distillate thus serves to produce squalene which will be isolated from a first fraction, with a second fraction of residual hydrocarbons.
  • the residue of the third distillation will be used for the production of sterols and vitamin E.
  • the process thus makes it possible to extract each of the four unsaponifiables without any solvent of petroleum origin and to claim the labels of products obtained by natural physical and chemical processes.
  • a first extraction step is generally carried out with methanol / chloroform (2: 1) on the lipids recovered after cell lysis, followed by a chromatography step.
  • Extraction with supercritical CO 2 is in turn often preferred to minimize the use of organic solvents, as for example the article by BHATTACHARJEE and SINGHAL, in World Journal of Microbiology and Biotechnology, 2003, 19-6, pp 605-608.
  • This process comprises the following four steps: saponification, cracking, esterification of fatty acids and extraction by supercritical fluid.
  • this technology has the merit of proposing a much more efficient method than HPLC (high pressure liquid chromatography) more conventional, because it offers a unique chromatographic partition liquid / liquid without solid support (and therefore without loss of material adsorption irreversible on said solid support).
  • the present invention therefore relates to a process for the preparation of a high squalene rich composition produced by fermentation of microorganisms, characterized in that it comprises a purification step chosen from the group consisting of extraction by supercritical CO 2 on a multistage fractionation column running countercurrently with reflux of extract, and molecular distillation called "short path”.
  • microorganisms are preferably microalgae belonging to the family Thraustochytriales sp. , more preferably microalgae belonging to the species Schizochytrium sp. , Aurantiochytrium sp. and Thraustochytrium sp.
  • composition of high squalene richness is intended to mean a composition having a squalene content of greater than 95% by weight, preferably greater than 97% by weight, more preferably still more preferably order of 100% by weight.
  • the first step of this first preferred mode is to prepare a biomass of microalgae belonging to the family Thraustochytriales.
  • strains belonging to the family Thraustochytriales are for example available:
  • the applicant company also has its own production strain, a Schizochytrium sp. filed on April 14, 2011 in France with the National Collection of Microorganism Cultures of the Institut Pasteur under number CNCM 1-4469 and also filed in China with the CHINA CENTER FOR TYPE CULTURE COLLECTION of Wuhan University, Wuhan 430072, PR China under the number M 209118.
  • the culture is carried out in heterotrophic conditions.
  • the culture step comprises a preculture step, to revive the strain, and then a culture or fermentation step itself. This last step corresponds to the production step of the lipid compounds of interest.
  • the second step of this first preferred mode is to treat the biomass so as to obtain a crude oil containing at least 10% by weight of squalene, preferably at least 15% by weight of squalene.
  • This enrichment means a squalene content of at least 10% by weight, preferably at least 15% by weight.
  • the third step of this first preferred embodiment consists of fractioning the crude oil thus obtained by contact with a supercritical pressure fluid on a multi-stage fractionation column operating countercurrently with reflux of extract so as to produce an extract having a high squalene between 70 and 75% and a raffinate with less than 1.5% squalene
  • the Applicant Company found that the use of a multistage fractionation column running countercurrently with an extract reflux, column with a structured packing, allowed to reach unexpectedly the squalene to high purity with excellent performance compared to the starting oil.
  • the solvent power can be finely adjusted by varying the pressure and temperature of the fluid.
  • the applicant company thus recommends using preferentially pure carbon dioxide, rather than added co-solvent which would increase its solvent power. It is also chosen an operating pressure of between 10 and 50 MPa, preferably between 15 and 25 MPa, and a temperature between 40 and 80 ° C.
  • the supercritical pressure fluid is pumped at high pressure by a pump and brought to the desired temperature in a heat exchanger before being injected at the bottom of the column at a flow rate kept constant and displayed on a mass flow meter.
  • the feed is injected via a high pressure pump in the middle of the column with structured packing, between sections 1 and 2, or 2 and 3, or 3 and 4, counted from the bottom of the column, at a flow rate kept constant and displayed on a mass flow meter.
  • the fluid loaded with the extract exits at the top of the column after which it is partially decompressed towards 6 MPa and sent to several separation stages, comprising in particular cyclonic separators mounted in series, whose body is heated by circulation of water in a reactor. Double envelope.
  • the liquid extract is recovered at the bottom of these separators while the fluid in the gaseous state is then recycled in a conventional manner: condensation in a condenser cooled to 0 to 5 ° C, intermediate storage in a buffer tank whose liquid level is kept constant by supplying fresh fluid from external storage, pumping at high pressure and reheating to the desired temperature.
  • the raffinate is discharged at the bottom of the column via an expansion valve controlled by a level probe, thus maintaining the oil-fluid interface in the lower part of the column; in order to avoid pressure surges that are detrimental to fractionation in the column, this raffinate is collected in two series-settling vessels in series, the pressure in the first being maintained at a value of about 1 to 4 MPa below the pressure in the column.
  • the reflux of the extract contributes significantly to improving the overall selectivity of the fractionation operation.
  • the reflux of extract is here caused and is carefully controlled by the establishment of a thermal gradient along the column when the diameter thereof allows a good heat transfer to the walls, between the fluid on the one hand contact with the load and secondly, the hot water circulating in the double-envelope divided into several independent sections to allow the implementation of this gradient.
  • supercritical pressure fluids have excellent heat and material transfer properties, far superior to those of liquids, contributing to the excellent selectivity observed.
  • the fourth step of this first preferred embodiment consists in bringing the thus-obtained extract into contact with a supercritical pressure fluid on the same multi-stage fractionation column operating against the flow with reflux of extract as that of step 3). in order to obtain a squalene content of between 95 and 99% by weight.
  • This squalene enrichment step is conducted under conditions similar to those of the previous step, but under slightly different pressure and temperature conditions.
  • An operating pressure of between 10 and 30 MPa, preferably between 10 and 20 MPa, and temperatures between 40 and 80 ° C. are thus chosen.
  • the fifth step of this first preferred embodiment is finally to collect the squalene composition thus obtained.
  • composition thus purified may contain a squalene content greater than or equal to 97%.
  • a method is implemented characterized in that it comprises the following steps:
  • the crude oil thus obtained consists of glycerides (predominant triglycerides), unsaponifiables (squalene majority) and possibly free fatty acids and phospholipids in smaller proportions.
  • This crude oil can be subjected to a crude refining before its extraction of squalene by molecular distillation.
  • Deodorization by vacuum distillation, called vapor stripping.
  • the fourth step of this second preferred mode of the process according to the invention consists in extracting squalene by molecular distillation known as "short path" so as to obtain a light fraction having a squalene content of greater than 60% by weight, preferably greater than 80% by weight.
  • the squalene of the optionally refined crude oil is extracted by molecular distillation.
  • the boiling point of squalene is of the order of 200 ° C.
  • This high vacuum makes it possible to limit the temperature and thus limit the risks of degradation / polymerization of squalene.
  • the residence time is kept very low, less than one minute.
  • the triglyceride fraction (high molecular mass) is not volatile.
  • the oil is pumped through a first thermostatically controlled circuit in a range of 25 to 100 ° C to the degasser (removal of traces of water and solvent).
  • the oil is pumped into the evaporation chamber ("short path") through a thermostatically controlled circuit in a temperature range of 50 to 150 ° C.
  • the temperature of the evaporator is adjusted in a range from 150 to 250 ° C.
  • the condenser is set in a temperature range of 0 to 50 ° C.
  • the pressure in the evaporation chamber is adjusted in a range of 10 ⁇ 2 to 10 ⁇ 4 mbar.
  • the distillate containing predominantly squalene and the residue containing predominantly triglycerides are conveyed via the collection circuits to the inert storage tanks.
  • the squalene content in the light fraction of the distillate is greater than 60% by weight, preferably greater than 80% by weight.
  • the fifth step of this second preferred embodiment of the process according to the invention consists in refining this light fraction by a series of saponification steps, biphasic separation, washing, decolourisation and deodorization, so as to obtain a raffinate having a squalene content. between 95 and 100%.
  • the saponification is carried out beforehand in order to hydrolyze the residual glycerides possibly entrained during the distillation but also to hydrolyze the esterified sterols.
  • the saponification is carried out with ethanolic potassium hydroxide at a temperature of approximately 80 ° C. over a period of 0.5 to 2 hours. After cooling, the two phases of the mixture resulting from the saponification can then be separated by decantation or centrifugation.
  • the ethanolic phase concentrates the free fatty acids but also a part of the polar impurities generated.
  • the oil phase concentrates squalene.
  • Basic water may be used to entrain residual saponification impurities during the first wash cycle (s).
  • Washing is terminated when the supernatant from the water wash is at neutral pH.
  • the squalene fraction is purified from a portion of the residual sterols as well as glycerides (mono-di-triglycerides).
  • An additional bleaching step can be performed at this stage to reduce the yellowish discolouration.
  • This bleaching step is carried out on activated charcoal in a manner similar to the discoloration conventionally used in vegetable oil refining.
  • the refining of the squalene fraction ends with a deodorization step.
  • the deodorization is carried out by steam “stripping" under hot vacuum (150-200 ° C.) over a period of 0.5 to 1 h.
  • the squalene thus purified is stored under a controlled atmosphere (ideally inerted with nitrogen).
  • antioxidants may be favorable for the stabilization of this fraction.
  • the invention also relates to the use of a squalene composition obtained by the implementation of a method according to the invention, in the cosmetic, pharmaceutical and medical fields.
  • the invention furthermore relates to a process for preparing a composition enriched with squalane by hydrogenation of the high purity squalene composition obtained by the implementation of a process according to the invention, as well as the use of this composition. of squalane in the cosmetic field.
  • This example illustrates the process of extracting an oil enriched with squalene produced by fermentation of the microalgae Schizochytrium sp. belonging to the company Applicant (filed on April 14, 2011 in France with the National Collection of Cultures of Microorganisms of the Pasteur Institute under number CNCM 1-4469).
  • the fermentation was conducted here in two successive preculture phases prior to the culture / production phase proper in a 20 1 reactor.
  • the preculture media then had the composition presented in Tables I and II below:
  • Clerol antifoam "FBA3107” was used at 1 ml / l. Possibly 50 mg / l of Penicillin G "sodium knows” to prevent the growth of contaminating bacteria.
  • Glucose was sterilized with KH 2 PO 4 and separately from the rest of the medium since this prevented the formation of a precipitate (Ammonium-Phosphate-Magnesium).
  • the mixture of vitamins and trace elements were added after sterilizing filtration.
  • the composition of the culture / production medium is given in the following Table III.
  • composition of vitamin mixtures and trace elements is given in Tables IV and V below:
  • the first preculture was carried out in 500 ml Erlenmeyer flasks equipped with baffles, into which a drop of CLEAROL FBA 3107 antifoaming agent marketed by COGNIS GmbH Dusseldorf was added.
  • the culture medium was filtered after complete dissolution of its constituents, possibly supplemented with penicillin G "sodium knows" at a rate of 0.25 mg / l.
  • Inoculation was carried out by taking microalgae colonies grown in Petri dishes (at a rate of 10 ⁇ ).
  • the incubation lasted 24 to 36 hours, at a temperature of 28 ° C., with stirring at 100 rpm (on an orbital shaker).
  • Seeding was then done with 3 to 5 ml of the first preculture.
  • the actual culture was carried out as follows in a reactor of 20 liters.
  • Table IV below shows the results obtained Schizochytrium sp. of the applicant company.
  • the dry cell concentration on the total dry matter is 95%.
  • the washed biomass is stirred in a Fermentor 2 1 type laboratory reactor (such as those marketed by the company Interscience) equipped with a marine propeller and baffles.
  • a Fermentor 2 1 type laboratory reactor such as those marketed by the company Interscience
  • This system makes it possible to limit the emulsification of the generated cell lysate while allowing a good mixture essential for the action of the lytic enzyme.
  • the temperature is adjusted to 60 ° C and the pH is regulated to about 8 with sodium hydroxide.
  • the duration of the lysis is fixed at 4 h.
  • the lysate is centrifuged for 5 minutes at 12000 g.
  • the oil, containing the squalene, having phase shifted on the surface is thus extracted.
  • the biomass is extracted from the fermenter by a volumetric pump SEEPEX supplying a Flott eg S3E sedicant.
  • the biomass is concentrated in this way at 200 g / 1.
  • the concentrate is diluted in a 1 m 3 tank with decarbonated water (1 volume of water / volume of concentrate) and then reconcentrated by the same operation as that described previously to obtain 620 kg of washed biomass and concentrated to 110 g / 1 .
  • the biomass is stirred at 150 rpm in a 1 m 3 tank, and is heated to 60 ° C.
  • the pH is then adjusted to 8 at 45% potash.
  • the enzyme, NOVO Alcalase 2, 4L FG, is added at a level of 1% (/ dry biomass).
  • the lysis parameters are maintained for 6 hours.
  • the quality of the lysis is monitored by optical microscope and by centrifugation of samples (2 min, 10000 g).
  • Example 2 In the same way as in Example 1, the temperature is then raised to 80 ° C. and then centrifuged on ALPHA LAVAL CLARA 20 centrifugation module, configured in 3-outlet concentrator mode.
  • This configuration is particularly well suited for the separation of a three-phase mixture of solid / liquid / liquid type.
  • the cellular lysate feed is carried out using a volumetric pump at a flow rate of 100 to 400 l / h.
  • the interface between the heavy phase and the light phase is displaced by adjusting the heavy phase output counterpressure.
  • the self - cleaning frequency is set at a frequency of 2 to 15 minutes.
  • a crude oil containing 21.8% squalene is obtained by extraction from a biomass of microalgae prepared according to Example 2.
  • the oil passes through the evaporation chamber ("short path") through a circuit maintained at 85 ° C.
  • the temperature of the evaporator is adjusted to 220 ° C.
  • the condenser is set to a temperature of 20 ° C.
  • the vacuum in the evaporation chamber is pushed to the maximum ( ⁇ 10 ⁇ 3 mbar).
  • the distillate containing the squalene and the triglyceride-containing residue are fed via the collection circuits to the inert storage tanks. At this stage, about 1.5 kg of distillate and 6 kg of residue are recovered.
  • the squalene content (mass percentage resulting from an NMR analysis) in the distillate is equal to 94%.
  • the squalene content of the residue is less than 2%.
  • the saponification step is carried out in potassium medium (2N) in accordance with the ratio 1/2 (m hui e i / m potash and anoiique) with ethanolic solvent (9/1 (m ethano i / m water).
  • the saponification medium is maintained at 80 ° C. under reflux for 45 minutes.
  • the free fatty acid content thus increases from 0.29 to 3.1 (oleic acid / ⁇ gill).
  • the two phases of the partially emulsified saponification mixture are separated by centrifugation (10 min at 25,000 g).
  • the extracted oil phase (squalene) is washed with slightly potassée water (3/1 (m water / m hui e i).
  • the washing is repeated with pure water until a supernatant at neutral pH is obtained.
  • the separation between each washing step is carried out by centrifugation for 10 min at 25,000 g.
  • the fraction purified by saponification is decolorized with activated charcoal (5% / oil) with stirring and then the activated charcoal is separated by filtration at 0.2 ⁇ .
  • the final stage of deodorization is carried out by steam stripping at 180 ° C. under vacuum for 30 minutes.
  • the purified squalene thus obtained has a purity close to 98%.
  • This oil contains more particularly triglycerides mainly with fatty acids:
  • the goal is to obtain more than 95% purified squalene and an oil free of squalene.
  • the fractionation method implemented according to the invention thus comprises two steps that can be summarized as follows:
  • Step 1 Fractionation of the crude oil by contact with a supercritical pressure fluid delivering a squalene-rich extract and a squalene-free raffinate;
  • Step 2 Purification of squalene by fractionation of the extract obtained in step 1, by contact with a supercritical pressure fluid;
  • This fractionation is based on the important difference in solubility between squalene (non-polar hydrocarbon) and the triglycerides constituting the lipids of the oil, squalene being much more soluble than triglycerides.
  • the two fractionation steps are carried out on a packed fractionation column operating countercurrently with internal reflux of extract.
  • the fractionation unit used is equipped with a counter-current fractionation column with an internal diameter of 125 mm and a height of 8 m making it possible to establish a temperature gradient in 4 sections of 2 m.
  • This column is filled with high performance packing (type Sulzer BX). This unit is fully automated and allows continuous operation.
  • Step 1 Treatment of the crude oil to extract squalene
  • the oil is introduced into the column between sections 3 and 4, counted starting from the bottom of the column.
  • the process parameters are shown in the following Table V.
  • Squalene is thus recovered in the extract with a relatively high concentration.
  • Step 2 Purification of squalene:

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EP13720486.3A 2012-04-16 2013-04-15 Verfahren zum raffinieren von squalen aus mikroalgen Pending EP2838630A2 (de)

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FR1253496A FR2989373B1 (fr) 2012-04-16 2012-04-16 Procede de raffinage du squalene produit par microalgues
FR1253614 2012-04-19
PCT/FR2013/050812 WO2013156720A2 (fr) 2012-04-16 2013-04-15 Procédé de raffinage du squalène produit par microalgues

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TWI646189B (zh) * 2013-12-20 2019-01-01 荷蘭商Ｄｓｍ智慧財產有限公司 用於從微生物細胞獲得微生物油之方法（五）
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CA2869358A1 (fr) 2013-10-24
WO2013156720A2 (fr) 2013-10-24
US9346722B2 (en) 2016-05-24
CN104245076B (zh) 2017-03-01
US20150140030A1 (en) 2015-05-21
WO2013156720A3 (fr) 2014-01-09
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KR102192410B1 (ko) 2020-12-17
CN105296552A (zh) 2016-02-03

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