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WO2018122057A1 - Procédé d'isolement de lipides à partir d'une biomasse contenant des lipides - Google Patents

Procédé d'isolement de lipides à partir d'une biomasse contenant des lipides Download PDF

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Publication number
WO2018122057A1
WO2018122057A1 PCT/EP2017/083712 EP2017083712W WO2018122057A1 WO 2018122057 A1 WO2018122057 A1 WO 2018122057A1 EP 2017083712 W EP2017083712 W EP 2017083712W WO 2018122057 A1 WO2018122057 A1 WO 2018122057A1
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WO
WIPO (PCT)
Prior art keywords
suspension
hours
biomass
cells
pufas
Prior art date
Application number
PCT/EP2017/083712
Other languages
English (en)
Inventor
Michael Diehl
Xiao Daniel DONG
Annika HARTMANN
Martin Heining
Michael Benjamin Johnson
Jochen Lebert
Neil Francis Leininger
SR. Kirt Lyvell MATTHEWS
Mark Edward NEJAKO II
Holger Pfeifer
Christian Rabe
Shannon Elizabeth Ethier RESOP
Ginger Marie SHANK
Vinod Tarwade
David Allen Tinsley
Original Assignee
Evonik Degussa Gmbh
Dsm Ip Assets B.V.
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 Evonik Degussa Gmbh, Dsm Ip Assets B.V. filed Critical Evonik Degussa Gmbh
Priority to DK17825501.4T priority Critical patent/DK3562925T3/da
Priority to CN201780087448.3A priority patent/CN110462014A/zh
Priority to ES17825501T priority patent/ES2872009T3/es
Priority to RU2019123315A priority patent/RU2744913C2/ru
Priority to BR112019013418-2A priority patent/BR112019013418B1/pt
Priority to EP17825501.4A priority patent/EP3562925B1/fr
Priority to US16/473,805 priority patent/US11352651B2/en
Priority to CA3048289A priority patent/CA3048289C/fr
Publication of WO2018122057A1 publication Critical patent/WO2018122057A1/fr

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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
    • C11B1/00—Production of fats or fatty oils from raw materials
    • C11B1/10—Production of fats or fatty oils from raw materials by extracting
    • A—HUMAN NECESSITIES
    • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
    • A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS OR COOKING OILS
    • A23D9/00—Other edible oils or fats, e.g. shortenings or cooking oils
    • A23D9/02—Other edible oils or fats, e.g. shortenings or cooking oils characterised by the production or working-up
    • 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
    • C11B1/12—Production of fats or fatty oils from raw materials by melting out

Definitions

  • the current invention relates to a method of isolating polyunsaturated fatty acids containing lipids from a lipids containing biomass.
  • PUFAs polyunsaturated fatty acids
  • PUFAs containing lipids are of high interest in the feed, food and pharmaceutical industry. Due to overfishing there is a high need for alternative sources for PUFAs containing lipids besides fish oil. It turned out that besides certain yeast and algal strains in particular microalgal cells like those of the order Thraustochytriales are a very good source for PUFAs containing lipids.
  • a first subject of the current invention is a method of isolating a polyunsaturated fatty acids (PUFAs) containing lipid from a biomass, comprising the following steps:
  • TDM total dry matter
  • a particular subject of the current invention is a method of isolating a
  • polyunsaturated fatty acids PUFAs
  • PUFAs polyunsaturated fatty acids
  • TDM total dry matter
  • a temperature of 20°C to below 80°C preferably a temperature of 25°C to below 60°C, more preferably 25°C to 58°C, in particular 30 to 55°C, above all a temperature of 30°C to 50°C;
  • a further particular subject of the current invention is a method of isolating a polyunsaturated fatty acids (PUFAs) containing lipid from a biomass, comprising the following steps: a) Providing a suspension of a biomass comprising cells which contain a PUFAs containing lipid;
  • TDM total dry matter
  • a further subject of the current invention is a method of isolating a polyunsaturated fatty acids (PUFAs) containing lipid from a biomass, comprising the following steps: a) Providing a suspension of a biomass comprising cells which contain a PUFAs containing lipid;
  • TDM total dry matter
  • a further subject of the current invention is a method of isolating a polyunsaturated fatty acids (PUFAs) containing lipid from a biomass, comprising the following steps: a) Providing a suspension of a biomass comprising cells which contain a PUFAs containing lipid;
  • TDM total dry matter
  • the pH is according to the invention preferably kept in step (e) below 11.5, more preferably below 1 1, more preferably below 10.5, in particular in the range of 8 to 11.5, more preferably in the range of 9 to 11 , in particular in the range of 10 to 11. This is realized by adding the base in step (e) not at once, but either continuously or step by step, so that exceeding the indicated pH values can be avoided.
  • the steps (d) and (e) lead to the breaking of the emulsion as contained in the suspension into an oil containing light phase and a water, cell debris and salts containing heavy phase.
  • This breaking of the emulsion is also called “demulsification" in the context of this application.
  • the suspension is continuously mixed by using a stirrer and/or an agitator.
  • steps (d) and/or (e) preferably low shear agitation and/or axial- flow agitation is applied, in particular as disclosed in WO
  • Impellers suitable for agitating prior and during steps (d) and/or (e) include in particular straight blade impellers, Rushton blade impellers, axial flow impellers, radial flow impellers, concave blade disc impellers, high- efficiency impellers, propellers, paddles, turbines and combinations thereof.
  • base equivalent takes account of the fact that not only monovalent, but also bi- or multivalent bases do exist and can be used according to the invention.
  • a bivalent base is used instead or in addition to a monovalent base
  • only the half molar amount of this bivalent base has to be used to realize the same amount of base equivalents in comparison to the amount of monovalent base which would have to be used; in case a trivalent base is used, then only a third of the molar amount of monovalent base has to be used; etc.
  • a monovalent base like sodium hydroxide
  • the amount of base equivalents is identical to the amount of base.
  • the weight amount of base can easily be calculated basing on the molar amount by making use of the molar weight of the base. For example, in case of the very preferred base sodium hydroxide the molar weight equals to 40 g/mol. That means that one mole of sodium hydroxide corresponds to 40 g of sodium hydroxide.
  • Preferred bases as used according to the invention are selected from hydroxides, in particular sodium hydroxide, lithium hydroxide, potassium hydroxide, and/or calcium hydroxide, carbonates, in particular sodium carbonate, potassium carbonate, and/or magnesium carbonate, and/or bicarbonates, in particular lithium bicarbonate, sodium bicarbonate, and/or potassium bicarbonate.
  • the base used according to the invention is only or almost only sodium hydroxide.
  • the bases are preferably used in liquid form, in particular as concentrated solutions, wherein the concentration of base in the solution is preferably in the range of 10 to 60 wt.-%, in particular in the range of 20 to 50 wt.-%.
  • a lysing step is carried out.
  • the lysing step can be omitted, if - for example due to the fermentation conditions as applied - the cells or a big part thereof is already lysed or easily breakable in one of the following steps of the procedure without any explicit lysing step.
  • Lysing of the cells of the biomass according to step (b) can be carried out by methods as known to those skilled in the art, in particular enzymatically, mechanically, physically, or chemically, or by applying combinations thereof. Depending on the time of exposure and/or the degree of force applied, a composition comprising only lysed cells or a composition comprising a mixture of cell debris and intact cells may be obtained.
  • the term "lysed lipids containing biomass” insofar relates to a suspension which contains water, cell debris and oil as set free by the cells of the biomass, but beyond that may also comprise further components, in particular salts, intact cells, further contents of the lysed cells as well as components of a fermentation medium, in particular nutrients.
  • only small amounts of intact cells in particular less than 20 %, preferably less than 10 %, more preferably less than 5 % (relating to the total number of intact cells as present before lysing the cells of the biomass) are present in the lysed biomass after the step of lysing the cells.
  • Lysing of the cells may be realized for example by utilizing a French cell press, sonicator, homogenizer, microfluidizer, ball mill, rod mill, pebble mill, bead mill, high pressure grinding roll, vertical shaft impactor, industrial blender, high shear mixer, paddle mixer, and/or polytron homogenizer.
  • lysing of the cells comprises an enzymatic treatment of the cells by applying a cell- wall degrading enzyme.
  • the cell-wall degrading enzyme is preferably selected from proteases, cellulases (e.g., Cellustar CL (Dyadic), Fibrezyme G2000 (Dyadic), Celluclast (Novozymes), Fungamyl (Novozymes), Viscozyme L (Novozymes)), hemicellulases, chitinases, pectinases (e.g., Pectinex (Novozymes)), sucrases, maltases, lactases, alpha- glucosidases, beta-glucosidases, amylases (e.g., Alphastar Plus (Dyadic); Termamyl (Novozymes)), lysozymes, neuraminidases, galactosidases, alpha-mannosidases, glucuronidases, hyaluronidases, pullulanases, glucocerebro
  • the protease may be selected from serine proteases, threonine proteases, cysteine proteases, aspartate proteases, metalloproteases, glutamic acid proteases, alcalases (subtilisins), and combinations thereof.
  • the chitinase may be a chitotriosidase.
  • the pectinase may be selected from pectolyases, pectozymes,
  • the adequate pH for utilizing the enzyme depends on the pH optimum of the enzyme.
  • an enzyme with a pH optimum of between 7.0 and 8.0, in particular of about 7.5, is used, so that the pH applied in this step is from 7.0 to 8.0, preferably from 7.3 to 7.7.
  • a preferred enzyme which can be used in this pH range is an alcalase.
  • the enzyme is preferably added as a concentrated enzyme solution, preferably in an amount of 0.01 to 1.5 wt.-%, more preferably in an amount of 0.03 to 1.0 wt.-%, above all in an amount of 0.05 to 0.5 wt.-%, relating to the amount of concentrated enzyme solution as added in relation to the total amount of the suspension after addition of the concentrated enzyme solution.
  • lysing of the cells is carried out as follows: i) Heating the suspension of (a) to a temperature of between 50°C and 70°C,
  • the enzyme can be added before or after heating up the suspension and/or before or after adjusting the pH. In the same way heating up of the suspension can be carried out before or after adjusting the pH. - But in a preferred embodiment, the enzyme is added after heating up of the suspension and after adjusting the pH, if adjusting of the pH is necessary, at all. - In a very preferred embodiment all measures are carried out more or less simultaneously.
  • the suspension is continuously mixed by using a stirrer and/or an agitator.
  • the demulsification is carried out with a suspension having a dry matter content of 20 to 60 wt.-%, preferably 25 to 60 wt.%, in particular 30 to 55 wt.- % or 30 to 45 wt.-%.
  • a suspension having a dry matter content of 20 to 60 wt.-%, preferably 25 to 60 wt.%, in particular 30 to 55 wt.- % or 30 to 45 wt.-%.
  • This can be realized by either providing a suspension with an appropriately high biomass in step (a) or by concentrating the suspension, in particular after lysing the cells of the biomass.
  • the suspension is concentrated to a total dry matter content of 20 to 60 wt.-%, more preferably 25 to 60 wt.-%, in particular 30 to 55 wt.-%, above all 30 to 50 wt.-% or 30 to 45 wt.-%.
  • Concentration of the suspension is preferably carried out by evaporation of water at a temperature not higher than 100°C, preferably 70°C to 100°C, more preferably 80°C to 90°C, until a total dry matter content of 20 to 60 wt.-% more preferably 25 to 60 wt.-%, in particular 30 to 55 wt.-% or 30 to 45 wt.-%, is reached.
  • Concentration of the suspension is preferably carried out in a forced circulation evaporator (for example available from GEA, Germany) to allow fast removal of the water.
  • concentration might be carried out by falling film evaporation, thin film evaporation and/or rotary evaporation.
  • adjusting the pH value can be carried out according to the invention by using either bases or acids as known to those skilled in the art. Decreasing of the pH can be carried out in particular by using organic or inorganic acids like sulfuric acid, nitric acid, phosphoric acid, boric acid, hydrochloric acid, hydrobromic acid, perchloric acid, hypochlorous acid, chlorous acid, fluorosulfuric acid, hexafluorophosphoric acid, acetic acid, citric acid, formic acid, or combinations thereof.
  • hydrochloric acid is the preferred substance for decreasing the pH value.
  • organic or inorganic bases like hydroxides, in particular sodium hydroxide, lithium hydroxide, potassium hydroxide, and/or calcium hydroxide, carbonates, in particular sodium carbonate, potassium carbonate, or magnesium carbonate, and/or bicarbonates, in particular lithium bicarbonate, sodium bicarbonate, and/or potassium bicarbonate.
  • the acids and bases are preferably used in liquid form, in particular as concentrated solutions, wherein the concentration of acid or base in the solution is preferably in the range of 10 to 55 wt.-%, in particular in the range of 20 to 50 wt.-%.
  • sulfuric acid is preferably used also in concentrated form.
  • the method according to the invention preferably comprises as a further step the harvesting of the PUFAs containing lipid from the demulsified composition as obtained in step (e).
  • the harvesting of the PUFAs containing lipid preferably comprises neutralization of the demulsified suspension and subsequent separation of the thus obtained oil containing light phase from the water, salts, cell debris and residual oil containing heavy phase.
  • Neutralization of the demulsified composition is preferably realized by adding an acid, preferably sulfuric acid, to adjust a pH value of 5.5 to 8.5, in particular 6.5 to 8.5, preferably 6.5 to 7.5 or 7.0 to 8.0. Before starting separation of the light phase from the heavy phase the neutralized composition may be stirred at this neutralized pH from several minutes up to several hours. - Neutralization of the demulsified composition is only necessary in this embodiment for sure, if the demulsified composition as obtained according to step (e) of the methods of the invention has a pH value outside of this range.
  • Separation of the oil containing light phase from the water, salts and cell debris containing heavy phase is preferably realized by mechanical means and preferably at a temperature of 60-90°C, more preferably 70-80°C, and preferably at a pH value of 6-9, more preferably 7- 8.5.
  • Mechanical means refers in particular to filtration and centrifugation methods as known to those skilled in the art.
  • the PUFAs containing oil thus obtained can further be worked up by applying methods as known to those skilled in the art, in particular refining, bleaching, deodorizing and/or winterizing.
  • a particular advantage of the method of the current invention is that it can be carried out without the use of any organic solvent, in particular without the use of any polar or non- polar organic solvent.
  • no or only little amounts of organic solvents are used for isolating the PUFAs containing oil from the biomass.
  • Typical organic solvents are hexane and ethanol.
  • less than 2 wt.-% non-polar organic solvents are used, more preferably less than 1, 0.5 or 0.1 wt.-%.
  • no non-polar organic solvent is used, at all.
  • organic solvents are used, in general, particularly preferred less than 1, 0.5 or 0.1 wt.-%. In a particularly very preferred embodiment of the invention no organic solvents are used, at all.
  • a further advantage of the method of the current invention is that a very efficient separation of the oil from the remaining biomass can be realized without the addition of sodium chloride, which is normally used for salting out the oil from the biomass.
  • the method can be carried out without the addition of chloride salts, at all, above all without the addition of any salts for salting out the oil.
  • chloride salts in particular sodium chloride, might be present in the suspension due to the fermentation medium as used for growing of the biomass.
  • no or only little amounts of sodium chloride are used for improving the oil isolation.
  • less than 1 wt.-% of sodium chloride are used, more preferably less than 0.5 or 0.2 wt.-% of sodium chloride are used for isolating the oil from the biomass, above all less than 0.1 or 0.05 wt.-%, wherein the wt.-% relate to the total weight of the composition after addition of the sodium chloride.
  • no or only little amounts of chloride salts are used for improving the oil isolation, at all.
  • no or only little amounts of salts are used for improving the oil isolation, in general.
  • the methods of the current invention allow a very efficient separation of the oil contained in the biomass from the cell-debris and other substances as contained in the suspension, in particular fermentation broth.
  • preferably more than 80 wt.-%, in particular more than 90 wt.-% of the oil contained in the biomass can be separated from the biomass and isolated by applying very economic and sustainable conditions.
  • Chloride refers to the amount of detectable chlorine.
  • the amount of chlorine as present can be determined for example by elemental analysis according to DIN EN ISO 11885.
  • the chlorine is present in the form of salts which are called “chlorides”.
  • the content of chloride as mentioned according to the invention also called “chloride ions” - only refers to the amount of detectable chlorine, not to the amount of the complete chloride salt, which comprises besides the chloride ion also a cationic counterion.
  • the total dry matter content (TDM) is preferably determined by gravimetric analysis. For doing that, a sample of the homogeneous suspension with a specific volume is weighed before and after freeze-drying. The remaining weight of the dried sample corresponds to the total dry matter as contained in that specific volume of the suspension.
  • the yield of liberated oil is preferably determined by fatty acid methyl ester analysis (FAME).
  • FAME fatty acid methyl ester analysis
  • the lipids in the sample are first saponified with KOH. After that, the free fatty acids are methylated with MeOH.
  • the methylated fatty acids can then be determined and quantified by gas chromatography by using an internal standard.
  • the water, salts, residual oil and cell debris containing aqueous phase which is obtained as by-product in the oil harvesting step as described before, is converted into a dried biomass by drying the biomass to a total dry matter content of more than 90 wt.-%.
  • Conversion of the water, salts, remaining oil and cell debris containing heavy phase, which is obtained as by-product in the oil harvesting step, into a dried biomass by drying the biomass to a total dry matter content of more than 90 wt.-% can be carried out in different ways.
  • the transformation is carried out by concentration of the heavy phase to a dry matter content of 30-50 wt.-%, preferably 35-45 wt.-%, and subsequent spray granulation of the biomass by means of fluidized bed granulation.
  • Concentration of the heavy phase to a dry matter content of 30-50 wt.-% is preferably carried out by solvent evaporation, in particular vacuum evaporation, and/or by using a rotary evaporator, a thin- film evaporator or a falling-film evaporator.
  • solvent evaporation in particular vacuum evaporation, and/or by using a rotary evaporator, a thin- film evaporator or a falling-film evaporator.
  • a useful alternative to solvent evaporation is reverse osmosis.
  • an anti-caking agent in particular silica, preferably a hydrophobic or hydrophilic silica
  • the suspension, in particular fermentation broth, comprising biomass as well as the silica are preferably sprayed into the particular drying zone.
  • the biomass may be mixed with the anti-caking agent after the drying process.
  • carboxymethylcellulose being a particulary preferred binding agent.
  • the dried biomass is preferably stored or packed.
  • the particulate biomass of the invention as well as the aqueous suspensions of the invention can be used in different ways. For example, they can be used in order to produce a foodstuff or feedstuff. Alternatively they may be used directly as foodstuff or feedstuff.
  • a further subject matter of the present invention is therefore likewise a method for producing a feedstuff or foodstuff, in which a particulate biomass and/or an aqueous suspension according to the invention is used, and is preferably mixed with further feedstuff or foodstuff ingredients.
  • the PUFAs containing cells of the biomass are preferably microbial cells or plant cells.
  • the cells are capable of producing the PUFAs due to a polyketide synthase system.
  • the polyketide synthase system may be an endogenous one or, due to genetic engineering, an exogenous one.
  • the plant cells may in particular be selected from cells of the families Brassicaceae, Elaeagnaceae and Fabaceae.
  • the cells of the family Brassicaceae may be selected from the genus Brassica, in particular from oilseed rape, turnip rape and Indian mustard; the cells of the family Elaeagnaceae may be selected from the genus Elaeagnus, in particular from the species Oleae europaea; the cells of the family Fabaceae may be selected from the genus Glycine, in particular from the species Glycine max.
  • the microbial organisms which contain a PUFAs containing lipid are described extensively in the prior art.
  • the cells used may, in this context, in particular be cells which already naturally produce PUFAs (polyunsaturated fatty acids); however, they may also be cells which, as the result of suitable genetic engineering methods or due to random mutagenesis, show an improved production of PUFAs or have been made capable of producing PUFAs, at all.
  • the production of the PUFAs may be auxotrophic, mixotrophic or heterotrophic.
  • the biomass preferably comprises cells which produce PUFAs heterotrophically.
  • the cells according to the invention are preferably selected from algae, fungi, particularly yeasts, bacteria, or protists.
  • the cells are more preferably microbial algae or fungi.
  • Suitable cells of oil-producing yeasts are, in particular, strains of Yarrowia, Candida, Rhodotorula, Rhodosporidium, Cryptococcus, Trichosporon and Lipomyces.
  • Suitable cells of oil-producing microalgae and algae-like microorganisms are, in particular, microorganisms selected from the phylum Stramenopiles (also called Heterokonta).
  • the microorganisms of the phylum Stramenopiles may in particular be selected from the following groups of microorganisms: Hamatores, Proteromonads, Opalines,
  • microalgae include the members of the green algae and dinoflagellates, including members of the genus
  • the biomass according to the invention preferably comprises cells, and preferably consists essentially of such cells, of the taxon Labyrinthulomycetes (Labyrinthulea, net slime fungi, slime nets), in particular those from the family of Thraustochytriaceae.
  • the family of the Thraustochytriaceae includes the genera Althomia, Aplanochytrium, Aurantiochytrium, Botryochytrium, Elnia, Japonochytrium, Oblongichytrium,
  • the biomass particularly preferably comprises cells from the genera Aurantiochytrium, Oblongichytrium, Schizochytrium, or Thraustochytrium, above all from the genus
  • the polyunsaturated fatty acid is preferably a highly-unsaturated fatty acid (HUFA).
  • the cells present in the biomass are preferably distinguished by the fact that they contain at least 20% by weight, preferably at least 30%> by weight, in particular at least 35% by weight, of PUFAs, in each case based on cell dry matter.
  • lipid includes phospholipids; free fatty acids; esters of fatty acids; triacylglycerols; sterols and sterol esters; carotenoids;
  • xanthophylls e. g. oxycarotenoids
  • hydrocarbons isoprenoid-derived compounds and other lipids known to one of ordinary skill in the art.
  • lipid and “oil” are used interchangeably according to the invention.
  • the majority of the lipids in this case is present in the form of triglycerides, with preferably at least 50% by weight, in particular at least 75% by weight and, in an especially preferred embodiment, at least 90% by weight of the lipids present in the cell being present in the form of triglycerides.
  • polyunsaturated fatty acids PUFAs
  • HUFAs highly-unsaturated fatty acids
  • HUFAs are understood to mean fatty acids having at least four C-C double bonds.
  • the PUFAs may be present in the cell in free form or in bound form.
  • Examples of the presence in bound form are phospholipids and esters of the PUFAs, in particular monoacyl-, diacyl- and triacylglycerides.
  • the majority of the PUFAs is present in the form of triglycerides, with preferably at least 50% by weight, in particular at least 75% by weight and, in an especially preferred embodiment, at least 90% by weight of the PUFAs present in the cell being present in the form of triglycerides.
  • Preferred PUFAs are omega-3 fatty acids and omega-6 fatty acids, with omega-3 fatty acids being especially preferred.
  • Preferred omega-3 fatty acids here are the
  • eicosapentaenoic acid (EPA, 20:5 ⁇ -3), particularly the (5Z,8Z,1 lZ,14Z,17Z)-eicosa- 5,8,11 , 14, 17-pentaenoic acid, and the docosahexaenoic acid (DHA, 22:6 ⁇ -3), particularly the (4Z,7Z,10Z,13Z,16Z,19Z)-docosa-4,7,10,13,16,19-hexaenoic acid.
  • DHA docosahexaenoic acid
  • cells in particular a
  • Schizochytrium strain which produces a significant amount of EPA and DHA, simultaneously, wherein DHA is preferably produced in an amount of at least 20 wt.-%, preferably in an amount of at least 30 wt.-%, in particular in an amount of 30 to 50 wt.-%, and EPA is produced in an amount of at least 5 wt.-%, preferably in an amount of at least 10 wt.-%, in particular in an amount of 10 to 20 wt.-% (in relation to the total amount of lipid as contained in the cells, respectively).
  • DHA and EPA producing Schizochytrium strains can be obtained by consecutive mutagenesis followed by suitable selection of mutant strains which demonstrate superior EPA and DHA production and a specific EPA:DHA ratio.
  • Any chemical or nonchemical (e.g. ultraviolet (UV) radiation) agent capable of inducing genetic change to the yeast cell can be used as the mutagen.
  • UV radiation ultraviolet
  • These agents can be used alone or in combination with one another, and the chemical agents can be used neat or with a solvent.
  • PTA-10208 PTA-10209, PTA-10210, or PTA-10211, PTA-10212, PTA-10213, PTA-10214, PTA-10215.
  • the suspension of bio mass according to the present invention has preferably a bio mass density of at least 80 or 100 g/1, in particular a biomass density of 80 to 250 g/1, in particular 80 to 200 g/1, more preferably a biomass density of at least 120 or 140 g/1, in particular at least 160 or 180 g/1 (calculated as dry-matter content) and is preferably a fermentation broth.
  • the suspension may be obtained by culturing and growing suitable cells in a fermentation medium under conditions whereby the PUFAs are produced by the microorganism.
  • Methods for producing the biomass, in particular a biomass which comprises cells containing lipids, in particular PUFAs, particularly of the order Thraustochytriales, are described in detail in the prior art (see e.g.
  • the production takes place by cells being cultured in a fermenter in the presence of a carbon source and of a nitrogen source, along with a number of additional substances like minerals that allow growth of the microorganisms and production of the PUFAs.
  • biomass densities of more than 100 grams per litre and production rates of more than 0.5 gram of lipid per litre per hour may be attained.
  • the process is preferably carried out in what is known as a fed-batch process, i.e. the carbon and nitrogen sources are fed in incrementally during the fermentation.
  • lipid production may be induced by various measures, for example by limiting the nitrogen source, the carbon source or the oxygen content or combinations of these.
  • the cells are grown until they reach a biomass density of at least 80 or 100 g/1, more preferably at least 120 or 140 g/1, in particular at least 160 or 180 g/1 (calculated as total dry matter content).
  • a biomass density of at least 80 or 100 g/1, more preferably at least 120 or 140 g/1, in particular at least 160 or 180 g/1 (calculated as total dry matter content).
  • the cells are fermented in a medium with low salinity, in particular so as to avoid corrosion. This can be achieved by using chlorine-free sodium salts as the sodium source instead of sodium chloride, such as, for example, sodium sulphate, sodium carbonate, sodium hydrogen carbonate or soda ash.
  • chloride is used in the fermentation in amounts of less than 3 g/1, in particular less than 500 mg/1, especially preferably less than 100 mg/1.
  • Suitable carbon sources are both alcoholic and non-alcoholic carbon sources.
  • alcoholic carbon sources are methanol, ethanol and isopropanol.
  • nonalcoholic carbon sources are fructose, glucose, sucrose, molasses, starch and corn syrup.
  • Suitable nitrogen sources are both inorganic and organic nitrogen sources.
  • inorganic nitrogen sources are nitrates and ammonium salts, in particular ammonium sulphate and ammonium hydroxide.
  • organic nitrogen sources are amino acids, in particular glutamate, and urea.
  • inorganic or organic phosphorus compounds and/or known growth-stimulating substances such as, for example, yeast extract or corn steep liquor, may also be added so as to have a positive effect on the fermentation.
  • the cells are preferably fermented at a pH of 3 to 11, in particular 4 to 10, and preferably at a temperature of at least 20°C, in particular 20 to 40°C, especially preferably at least 30°C.
  • a typical fermentation process takes up to approximately 100 hours.
  • the cells may be pasteurized in order to kill the cells and to deactivate enzymes which might promote lipid degradation.
  • the pasteurization is preferably effected by heating the biomass to a temperature of 50 to 121°C, preferably 50 to 70°C, for a period of 5 to 150 minutes, in particular 20 to 100 minutes.
  • antioxidants may be added in order to protect the PUFAs present in the biomass from oxidative degradation.
  • Preferred antioxidants in this context are BHT, BHA, TBHA, ethoxyquin, beta-carotene, vitamin E, in particular tocopherol, and vitamin C.
  • the antioxidant if used, is preferably added in an amount of 0.001 to 0.1 wt.-%, preferably in an amount of 0.002 to 0.05 wt.-%, relating to the total amount of the fermentation broth after addition of the antioxidant.
  • Example 1 Preparation of the suspension for use in the demulsification tests
  • Example 5 Influence of the amount of added base equivalents on the liberation of the oil To test the significance of the amount of added base equivalents on the efficiency of the oil liberation from the biomass, the effect of addition of different amounts of caustic soda to the biomass with respect to the liberation of oil was tested. The ratio of base equivalents added to total dry matter is depicted in table 4 as well as the amount of oil as set free by the addition of the caustic soda. All experiments were carried out with one liter of
  • TDM total dry matter content
  • amount of base euqivalents and stirring speed on the liberation of the oil tests were carried out with enzymatically treated fermentation broths which were concentrated by forced circulation evaporation to a total dry matter content of either 25, 30 or 35 wt.-%. Tests were carried out in a stirring vessel BIOSTAT® B-DCU-Quad 2L (Sartorius, Germany). The volume of the concentrated suspensions as used in the tests was 1 L for each sample. In the tests the total amount of base equivalent added was varied from 5 to 7 wt.-%, while the demulsification was carried out either at 70, 80 or 90°C.
  • Example 7 Influence of temperature on the liberation of the oil
  • tests were carried out with enzymatically treated fermentation broths which were concentrated by forced circulation evaporation to a total dry matter content of 33 wt.-%. Tests were carried out in a stirring vessel BIOSTAT® B-DCU-Quad 2L (Sartorius, Germany). The volume of the concentrated suspensions as used in the tests was 1 L for each sample.
  • the same total amount of base equivalent (6 wt.-% NaOH per TDM, i.e. 15 moles NaOH per 10 kg TDM) was added, while the demulsification was carried out either at 40, 50 or 90°C.
  • the base equivalent was added in liquid form (20 wt.-% NaOH solution) in one shot at the beginning of the demulsification step. Demulsification took place at a stirrer speed of 300 rpm for 24 hours. After 24 hours the resulting composition was neutralized by adding sulfuric acid. After neutralization, a 50 g sample of the homogenized suspension was taken and separation of the cell debris was carried out by centrifugation at 13500 g. Subsequently the amount of EPA and DHA in the supernatant was determined. Table 6: Influence of the temperature on the yield of liberated oil
  • the base equivalent was added in liquid form (20 wt.-% NaOH solution) in one shot at the beginning of the demulsification step. Demulsification took place at a stirrer speed of 300 rpm for 24 hours. After 24 hours the resulting composition was neutralized by adding sulfuric acid. After neutralization, a 50 g sample of the homogenized suspension was taken and separation of the cell debris was carried out by centrifugation at 13500 g. Subsequently the amount of EPA and DHA in the supernatant was determined.
  • Enzymatically treated fermentation broths were concentrated by forced circulation evaporation to a total dry matter content of 34 wt.-%. Tests were carried out in a stirring vessel BIOSTAT® B-DCU-Quad 2L (Sartorius, Germany). The volume of the used concentrated suspensions was one liter for each sample. The demulsification was carried out at a temperature of 80°C and at an exposure time of 24 hours. The suspensions were stirred with 300 rpm. Either 10.6 moles base equivalents or 14.0 moles base equivalents of Ca(OH) 2 per 10 kg total dry matter were added to the suspension.
  • Ca(OH) 2 was added stepwise in suspended form (20 wt.-% Ca(OH) 2 in water) in the course of the exposure, so that the pH value of the suspension never exceeded pH 9.5. After the incubation the resulting composition was neutralized by adding sulfuric acid. After neutralization, a 50 g sample of the homogenized suspension was taken and separation of the cell debris was carried out by centrifugation at 13500 g. Subsequently the amount of EPA and DHA in the supernatant was determined.
  • Example 11 Demulsification without enzymatic treatment of the cells
  • tests were carried out with fermentation broths which after pasteurisation were not treated enzymatically, but directly concentrated by forced circulation evaporation to a total dry matter content of 32.8 wt.-%.
  • Tests were carried out in a stirring vessel BIOSTAT® B- DCU-Quad 2L (Sartorius, Germany). The volume of the used concentrated suspensions was 1 L for each sample. In each test the same total amount of base equivalent (6 wt.-% NaOH per TDM, i.e.

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Abstract

La présente invention concerne un procédé d'isolement de lipides contenant des acides gras polyinsaturés à partir d'une biomasse contenant des lipides.
PCT/EP2017/083712 2016-12-27 2017-12-20 Procédé d'isolement de lipides à partir d'une biomasse contenant des lipides WO2018122057A1 (fr)

Priority Applications (8)

Application Number Priority Date Filing Date Title
DK17825501.4T DK3562925T3 (da) 2016-12-27 2017-12-20 Fremgangsmåde til isolering af lipider fra en lipidholdig biomasse
CN201780087448.3A CN110462014A (zh) 2016-12-27 2017-12-20 从含有脂质的生物质中分离脂质的方法
ES17825501T ES2872009T3 (es) 2016-12-27 2017-12-20 Método de aislamiento de lípidos a partir de una biomasa que contiene lípidos
RU2019123315A RU2744913C2 (ru) 2016-12-27 2017-12-20 Способ выделения липидов из липидсодержащей биомассы
BR112019013418-2A BR112019013418B1 (pt) 2016-12-27 2017-12-20 Método de isolamento de lipídios a partir de uma biomassa contendo lipídios
EP17825501.4A EP3562925B1 (fr) 2016-12-27 2017-12-20 Procédé d'isolation de lipides à partir de biomasse contenant des lipides
US16/473,805 US11352651B2 (en) 2016-12-27 2017-12-20 Method of isolating lipids from a lipids containing biomass
CA3048289A CA3048289C (fr) 2016-12-27 2017-12-20 Procede d'isolement de lipides a partir d'une biomasse contenant des lipides

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US201662439354P 2016-12-27 2016-12-27
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Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2019121752A1 (fr) * 2017-12-20 2019-06-27 Evonik Degussa Gmbh Procédé d'isolement des lipides présents dans une biomasse contenant des lipides
WO2019191544A1 (fr) * 2018-03-30 2019-10-03 Dsm Ip Assets B.V. Procédé d'obtention d'une huile microbienne et procédé de réduction d'émulsion par maintien d'une faible concentration de glucide
WO2020141206A1 (fr) * 2019-01-03 2020-07-09 Corbion Biotech Inc. Procédé de fabrication d'une suspension de cellule lysée
US20210100751A1 (en) * 2018-02-02 2021-04-08 Commonwealth Scientific and Industral Research Organisation Protecting a bioactive and/or precursor thereof
EA038909B1 (ru) * 2018-02-15 2021-11-08 Эвоник Оперейшенс ГмбХ Способ выделения липидов из липидсодержащей биомассы
WO2021254863A1 (fr) 2020-06-18 2021-12-23 Evonik Operations Gmbh Procédé d'isolement de lipides à partir d'une biomasse contenant des lipides
WO2021260087A1 (fr) 2020-06-24 2021-12-30 Fermentalg Procédé de culture de microorganismes pour l'accumulation de lipides
US11261400B2 (en) 2017-09-05 2022-03-01 Evonik Operations Gmbh Method of separating lipids from a lysed lipids containing biomass
US11414621B2 (en) 2018-05-15 2022-08-16 Evonik Operations Gmbh Method of isolating lipids from a lipids containing biomass with aid of hydrophobic silica
US11946017B2 (en) 2016-07-13 2024-04-02 Evonik Operations Gmbh Method of separating lipids from a lysed lipids containing biomass
US11976253B2 (en) 2018-05-15 2024-05-07 Evonik Operations Gmbh Method of isolating lipids from a lysed lipids containing biomass by emulsion inversion

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WO1994008467A1 (fr) 1992-10-16 1994-04-28 Omegatech, Inc. Procede de production heterotrophe de produits microbiens a l'aide de concentrations elevees d'acides gras omega-3 fortement insatures
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CA2951001A1 (fr) * 2014-06-17 2015-12-23 Neste Oyj Methode de recuperation de lipides a partir d'une biomasse microbienne
WO2016050560A1 (fr) 2014-10-02 2016-04-07 Evonik Degussa Gmbh Procédé de fabrication d'une biomasse granulée contenant une matière valorisable sensible à l'oxydation

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11946017B2 (en) 2016-07-13 2024-04-02 Evonik Operations Gmbh Method of separating lipids from a lysed lipids containing biomass
US11261400B2 (en) 2017-09-05 2022-03-01 Evonik Operations Gmbh Method of separating lipids from a lysed lipids containing biomass
US11542220B2 (en) 2017-12-20 2023-01-03 Evonik Operations Gmbh Method of isolating lipids from a lipids containing biomass
WO2019121752A1 (fr) * 2017-12-20 2019-06-27 Evonik Degussa Gmbh Procédé d'isolement des lipides présents dans une biomasse contenant des lipides
US20210100751A1 (en) * 2018-02-02 2021-04-08 Commonwealth Scientific and Industral Research Organisation Protecting a bioactive and/or precursor thereof
EA038909B1 (ru) * 2018-02-15 2021-11-08 Эвоник Оперейшенс ГмбХ Способ выделения липидов из липидсодержащей биомассы
WO2019191544A1 (fr) * 2018-03-30 2019-10-03 Dsm Ip Assets B.V. Procédé d'obtention d'une huile microbienne et procédé de réduction d'émulsion par maintien d'une faible concentration de glucide
US11414621B2 (en) 2018-05-15 2022-08-16 Evonik Operations Gmbh Method of isolating lipids from a lipids containing biomass with aid of hydrophobic silica
US11976253B2 (en) 2018-05-15 2024-05-07 Evonik Operations Gmbh Method of isolating lipids from a lysed lipids containing biomass by emulsion inversion
WO2020141206A1 (fr) * 2019-01-03 2020-07-09 Corbion Biotech Inc. Procédé de fabrication d'une suspension de cellule lysée
WO2021254863A1 (fr) 2020-06-18 2021-12-23 Evonik Operations Gmbh Procédé d'isolement de lipides à partir d'une biomasse contenant des lipides
WO2021260087A1 (fr) 2020-06-24 2021-12-30 Fermentalg Procédé de culture de microorganismes pour l'accumulation de lipides
FR3111912A1 (fr) 2020-06-24 2021-12-31 Fermentalg Procédé de culture de microorganismes pour l’accumulation de lipides
EP3933016A1 (fr) 2020-06-30 2022-01-05 Evonik Operations GmbH Procédé d'isolation de lipides à partir de biomasse contenant des lipides

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