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
  • C11B1/02—Pretreatment
• • 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
  • C12P7/00—Preparation of oxygen-containing organic compounds
  • C12P7/64—Fats; Fatty oils; Ester-type waxes; Higher fatty acids, i.e. having at least seven carbon atoms in an unbroken chain bound to a carboxyl group; Oxidised oils or fats
  • C12P7/6409—Fatty acids
  • C12P7/6427—Polyunsaturated fatty acids [PUFA], i.e. having two or more double bonds in their backbone
• • A—HUMAN NECESSITIES
  • A23—FOODS OR FOODSTUFFS; TREATMENT THEREOF, NOT COVERED BY OTHER CLASSES
  • A23D—EDIBLE OILS OR FATS, e.g. MARGARINES, SHORTENINGS, COOKING OILS
  • A23D9/00—Other edible oils or fats, e.g. shortenings, cooking oils
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/42—Separation; Purification; Stabilisation; Use of additives
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C51/00—Preparation of carboxylic acids or their salts, halides or anhydrides
  • C07C51/42—Separation; Purification; Stabilisation; Use of additives
  • C07C51/487—Separation; Purification; Stabilisation; Use of additives by treatment giving rise to chemical modification
• • C—CHEMISTRY; METALLURGY
  • C07—ORGANIC CHEMISTRY
  • C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
  • C07C57/00—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms
  • C07C57/02—Unsaturated compounds having carboxyl groups bound to acyclic carbon atoms with only carbon-to-carbon double bonds as unsaturation
  • C07C57/03—Monocarboxylic acids
• • 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
  • C11B1/02—Pretreatment
  • C11B1/025—Pretreatment by enzymes or microorganisms, living or dead
• • 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
• • 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
• • 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
  • C12N1/06—Lysis of microorganisms
  • C12N1/066—Lysis of microorganisms by physical methods

Definitions

• a microbial oil comprising one or more polyunsaturated fatty acids (PUFAs) from one or more microbial cells by lysing the cells to form a lysed cell composition, treating the lysed cell composition to form an oil-containing emulsion and then recovering the oil from the oil-containing emulsion.
• PUFAs polyunsaturated fatty acids
• a microbial oil comprising one or more PUFAs that is recovered from microbial cells by at least one process described herein.
• Microbial oil containing one or more PUFAs is produced by microorganisms, such as, for example, algae and fungi.
• a typical process for obtaining PUFA containing oil from microbial cells involves growing microorganisms that are capable of producing the desired oil in a fermentor, pond or bioreactor to produce a microbial cell biomass; separating the biomass from the fermentation medium in which the biomass was grown; drying the microbial cell biomass, using a water-immiscible organic solvent (e.g., hexane) to extract the oil from the dried cells; and removing the organic solvent (e.g., hexane) from the oil.
• This process can further involve diluting the fermentation medium containing the cell biomass with water followed by centrifugation to separate the biomass from the diluted fermentation medium.
• Another process for obtaining PUFA containing oil from microbial cells involves growing microorganisms that fare capable of producing the desired oil in a fermentor, pond or bioreactor to produce a microbial cell biomass; releasing the PUFA containing oil into the fermentation medium in which the cells were grown by using mechanical force (e.g., homogenization), enzymatic treatment, or chemical treatment to disrupt the cell walls; and recovering the oil from the resulting composition comprising PUFA containing oil, cell debris, and liquid using a water miscible organic solvent, e.g., isopropyl alcohol.
• the oil can be separated mechanically from the composition and the alcohol must be removed from both the oil and the aqueous biomass waste stream.
• the use of heat in the above processes to dry the cells and/or remove the solvent from the recovered oil can degrade the PUFA containing oils and increase energy usage, which can further increase processing costs. Degradation occurs when PUFA containing oils are exposed to oxygen such as when the integrity of the microbial cell walls is disrupted and/or the microbial cells are exposed to heat.
• a solvent-free process for obtaining PUFA containing oil from microbial cells involves growing microorganisms that are capable of producing the desired oil in a fermentor, pond or bioreactor to produce a microbial cell biomass; releasing the PUFA containing oil into the fermentation medium in which the cells were grown by using mechanical force (e.g., homogenization), enzymatic treatment, or chemical treatment to disrupt the cell walls; and recovering crude oil from the resulting composition comprising PUFA containing oil, cell debris, and liquid by raising the pH adding a salt, heating, and/or agitating the resulting composition.
• This solvent-free process for obtaining PUFA containing oil from cells can require long oil recovery times, large amounts of salt, and/or many steps, which can all increase processing costs.
• PUFAs polyunsaturated fatty acids
• PUFAs polyunsaturated fatty acids
• At least one of (a) or (b) further comprises raising the pH of the cells or lysed cell composition.
• PUFAs polyunsaturated fatty acids
• At least one of (a) or (b) further comprises heating the cells or lysed cell composition to at least 50° C.
• PUFAs polyunsaturated fatty acids
• At least one of (a) or (b) further comprises agitating the cells or lysed cell composition.
• PUFAs polyunsaturated fatty acids
• PUFAs polyunsaturated fatty acids
• PUFAs polyunsaturated fatty acids
• PUFAs polyunsaturated fatty acids
• (d) further comprises at least one of heating to at least 50° C., adding an acid and adding a base.
• PUFAs polyunsaturated fatty acids
• At least one of (a) and (b) comprises raising the pH of the cells or lysed cell composition, agitating the cells or lysed cell composition, and heating the cells or lysed cell composition.
• a microbial oil obtained by any of the processes described herein.
• PUFAs polyunsaturated fatty acids
• At least one of (a) or (b) further comprises raising the pH of the cells or lysed cell composition. In some embodiments, at least one of (a) or (b) further comprises agitating the cells or the lysed cell composition. In some embodiments, at least one of (a) or (b) further comprises heating the cells or lysed cell composition. In some embodiments, at least one of (a) or (b) further comprises at least one of raising the pH of the cells or lysed cell composition., agitating the cells or the lysed cell composition, and heating the cells or lysed cell composition.
• (a) further comprises adding an enzyme.
• (b) further comprises adding a salt.
• (c) further comprises heating. In some embodiments, (c) further comprises centrifuging.
• (d) further comprises heating. In some embodiments, (d) further comprises adding an acid. In some embodiments, (d) further comprises adding a base. In some embodiments, (d) further comprises adding an emulsifier.
• (e) further comprises centrifuging the oil. In some embodiments, (e) further comprises refining the oil.
• a microbial oil obtained by any of the processes described herein.
• Fatty acids are classified based on the length and saturation characteristics of the carbon chain.
• Fatty acids present in a microbial oil can have from 4 to 28 carbon atoms and are termed short chain, medium chain, or long chain fatty acids based on the number of carbons present in the chain.
• Fatty acids are termed saturated fatty acids when no double bonds are present between the carbon atoms, and are termed unsaturated fatty acids when double bonds are present.
• Unsaturated long chain fatty acids are monounsaturated when only one double bond is present and are polyunsaturated when more than one double bond is present.
• the microbial oil described herein refers to oil that comprises one or more PUFAs and is obtained from microbial cells.
• Polyunsaturated fatty acids are classified based on the position of the first double bond from the methyl end of the fatty acid; omega-3 (n-3) fatty acids contain a first double bond at the third carbon, while omega-6 (n-6) fatty acids contain a first double bond at the sixth carbon.
• DHA docosahexaenoic acid
• LC-PUFA omega-3 long chain polyunsaturated fatty acid
• the PUFA is selected from an omega-3 fatty acid, an omega-6 fatty acid, and mixtures thereof.
• the PUFA is selected from LC-PUFAs.
• the PUFA is selected from docosahexaenoic acid (DHA), eicosapentaenoic acid (EPA), docosapentaenoic acid (DPA), arachidonic acid (ARA), gamma-linolenic acid (GLA), dihomo-gamma-linolenic acid (DGLA), stearidonic acid (SDA), and mixtures thereof.
• DHA docosahexaenoic acid
• EPA eicosapentaenoic acid
• DPA docosapentaenoic acid
• ARA arachidonic acid
• GLA gamma-linolenic acid
• DGLA dihomo-gamma-linolenic acid
• SDA stearidonic acid
• the PUFA is selected from DHA, ARA, and mixtures thereof.
• the PUFA is DHA.
• the PUFA is ARA.
• LC-PUFAs are fatty acids that contain at least 3 double bonds and have a chain length of 18 or more carbons or 20 or more carbons.
• LC-PUFAs of the omega-6 series include, but are not limited to, di-homo-gammalinoleic acid (C20:3n-6), arachidonic acid (C20:4n-6) (“ARA”), docosatetraenoic acid or adrenic acid (C22:4n-6), and docosapentaenoic acid (C22:5n-6) (“DPA n-6”).
• the LC-PUFAs of the omega-3 series include, but are not limited to, eicosatrienoic acid (C20:3n-3), eicosatetraenoic acid (C20:4n-3), eicosapentaenoic acid (C20:5n-3) (“EPA”), docosapentaenoic acid (C22:5n-3), and docosahexaenoic acid (C22:6n-3).
• the LC-PUFAs also include fatty acids with greater than 22 carbons and 4 or more double bonds including, but not limited to, C24:6(n-3) and C28:8(n-3).
• the PUFAs can be in the form of a free fatty acid, salt, fatty acid ester (e.g. methyl or ethyl ester), monoacylglycerol (MAG), diacylglycerol (DAG), triacylglycerol (TAG), and/or phospholipid (PL).
• fatty acid ester e.g. methyl or ethyl ester
• MAG monoacylglycerol
• DAG diacylglycerol
• TAG triacylglycerol
• PL phospholipid
• Highly unsaturated fatty acids are omega-3 and/or omega-6 polyunsaturated fatty acids that contain 4 or more unsaturated carbon-carbon bonds.
• a “cell” refers to an oil-containing biomaterial, such as biomaterial derived from oleaginous microorganisms. Oil produced by a microorganism or obtained from a microbial cell is referred to as “microbial oil”. Oil produced by algae and/or fungi is also referred to as algal and/or fungal oil, respectively.
• a “microbial cell” or “microorganism” refers to organisms such as algae, bacteria, fungi, yeast, protist, and combinations thereof, e.g., unicellular organisms.
• a microbial cell is a eukaryotic cell.
• a microbial cell includes, but is not limited to, golden algae (e.g., microorganisms of the kingdom Stramenopiles); green algae; diatoms; dinoflagellates (e.g., microorganisms of the order Dinophyceae including members of the genus Crypthecodinium such as, for example, Crypthecodinium cohnii or C.
• microalgae of the order Thraustochytriales yeast (Ascomycetes or Basidiomycetes); and fungi of the genera Mucor, Mortierella , including but not limited to Mortierella alpina and Mortierella sect. schmuckeri , and Pythium , including but not limited to Pythium insidiosum.
• the microbial cells are from the genus Mortierella , genus Crypthecodinium , or order Thraustochytriales. In a still further embodiment, the microbial cells are from Crypthecodinium Cohnii . In yet an even further embodiment, the microbial cells are selected from Crypthecodinium Cohnii, Mortierella alpina , genus Thraustochytrium , genus Schizochytrium , and mixtures thereof.
• the microbial cells include, but are not limited to, microorganisms belonging to the genus Mortierella , genus Conidiobolus , genus Pythium , genus Phytophthora , genus Penicillium , genus Cladosporium , genus Mucor , genus Fusarium , genus Aspergillus , genus Rhodotorula , genus Entomophthora , genus Echinosporangium , and genus Saprolegnia .
• ARA is obtained from microbial cells from the genus Mortierella , which includes, but is not limited to, Mortierella elongata, Mortierella exigua, Mortierella hygrophila, Mortierella alpina, Mortierella schmuckeri , and Mortierella minutissima .
• ARA is obtained from microbial cells from Mortierella elongata IFO8570, Mortierella exigua IFO8571, Mortierella hygrophila IFO5941, Mortierella alpina IFO8568, ATCC16266, ATCC32221, ATCC42430, CBS219.35, CBS224.37, CBS250.53, CBS343.66, CBS527.72, CBS529.72, CBS608.70, and CBS754.68, and mutants thereof.
• the microbial cells are from Mortierella alpina.
• the microbial cells are from microalgae of the order Thraustochytriales, which includes, but is not limited to, the genera Thraustochytrium (species include arudimentale, aureum, benthicola, globosum, kinnei, motivum, multirudimentale, pachydermum, proliferum, roseum, striatum ); the genera Schizochytrium (species include aggregatum, limnaceum, mangrovei, minutum, octosporum ); the genera Ulkenia (species include amoeboidea, kerguelensis, minuta, profunda, radiate, sailens, sarkariana, schizochytrops, visurgensis, yorkensis ); the genera Aurantiacochytrium ; the genera Oblongichytrium ; the genera Sicyoidochytium ; the genera Parientichytrium ; the genera Botryochytrium
• the microbial cells are from the order Thraustochytriales. In yet another embodiment, the microbial cells are from Thraustochytrium . In still a further embodiment, the microbial cells are from Schizochytrium . In a still further embodiment, the microbial cells are chosen from genus Thraustochytrium, Schizochytrium , or mixtures thereof.
• the process comprises lysing microbial cells comprising a microbial oil to form a lysed cell composition.
• lyse and “lysing” refer to a process whereby the wall and/or membrane of the microbial cell is ruptured.
• the microbial cell is lysed by being subjected to at least one treatment selected from mechanical, chemical, enzymatic, physical, and combinations thereof.
• the process comprises lysing the microbial cells comprising the microbial oil to form a lysed cell composition, wherein the lysing is selected from mechanical, chemical, enzymatic, physical, and combinations thereof.
• the cell prior to lysing the cell, can be washed and/or pasteurized.
• washing the cells includes using an aqueous solution, such as water, to remove any extracellular water-soluble or water-dispersible compounds.
• the cell can be washed once, twice, thrice, or more.
• pasteurizing the cell includes heating the cell to inactivate any undesirable enzymes, for example any enzymes that might degrade the oil or reduce the yield of PUFAs.
• the cell is washed and then pasteurized before being lysed.
• the cells that are being lysed are contained in a fermentation broth.
• the process comprises lysing unwashed microbial cells comprising a microbial oil to form a lysed cell composition.
• a fermentation broth comprising microbial cells comprising microbial oil is first washed with, for example, water and then the cells lysed to form a lysed cell composition.
• the process comprises lysing unwashed cells in a fermentation medium to form a lysed cell composition.
• Mechanical treatment includes, but is not limited to, homogenization, ultrasound, cold-pressing, milling, and combinations thereof.
• the process comprises lysing the cells by homogenization. In some embodiments, the process comprises lysing the cell with a homogenizer.
• Homogenization includes, but is not limited to, processes that utilize 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, polytron homogenizer, industrial homogenizer (e.g., Niro Soavi VHP Homogenizer and APV Rannie and APV Gaulin homogenizers), Industrial high shear fluid processors (e.g., Microfluidics high shear fluid processor), cell lysing/bead mill homogenizers (e.g., Dyno-Mill and Buhler), and combinations thereof.
• the cells flow through a homogenizer that is optionally heated.
• suitable homogenization can include 1 to 3 passes through a homogenizer at either high and/or low pressures.
• the pressure during homogenization is 150 bar to 1,400 bar; 150 bar to 1,200 bar; 150 bar to 900 bar; 150 bar to 300 bar; 300 bar to 1,400 bar; 300 bar to 1,200 bar; 300 bar to 900 bar; 400 bar to 800 bar; 500 bar to 700 bar; or 600 bar.
• the pressure during homogenization is 2,000 psi to 20,000 psi; 2,000 psi to 18,000 psi; 2,000 psi to 16,000 psi; 2,000 psi to 14,000 psi; 2,000 psi to 12,000 psi; 2,000 psi to 10,000 psi; 2,000 psi to 8,000 psi; 2,000 psi to 6,000 psi; 2,000 psi to 4,000 psi; 4,000 psi to 20,000 psi; 4,000 psi to 18,000 psi; 4,000 psi to 16,000 psi; 4,000 psi to 14,000 psi; 4,000 psi to 12,000 psi; 4,000 psi to 10,000 psi; 4,000 psi to 8,000 psi; 4,000 psi to 6,000 psi; 4,000 psi to 14,000 p
• the microbial cells are mixed in high shear mixer before being homogenized.
• the high shear mixer is operated in a range of at least 5,000 rpm; at least 7,500 rpm; at least 10,000 rpm; at least 12,500 rpm; at least 15,000 rpm; 5,000 rpm to 15,000 rpm; 5,000 rpm to 12,500 rpm; 5,000 rpm to 10,000 rpm; 5,000 rpm to 7,500 rpm; 7,500 rpm to 15,000 rpm; 7,500 rpm to 12,500 rpm; 7,500 rpm to 10,000 rpm; 10,000 rpm to 15,000 rpm; 10,000 rpm to 12,500 rpm; or 12,500 rpm to 15,000 rpm.
• Physical treatment includes, but is not limited to, heating, which includes, but is not limited to, resistive, convection, steam, fluid bath, solar, and combinations thereof.
• the cells are heated in a tank with resistive coils in/on its walls.
• the cells are heated in a liquid bath with tubes passing there through.
• Chemical treatment includes, but is not limited to, raising the pH of the cells; lowering the pH of the cells; contacting the cells with a chemical; and combinations thereof.
• the cells are lysed by raising the pH of the cells.
• the pH is raised by adding a base.
• the bases include, but are not limited to, hydroxides (e.g., LiOH, NaOH, KOH, and Ca(OH) 2 , and combinations thereof); carbonates (e.g., Na 2 CO 3 , K 2 CO 3 , MgCO 3 , and combinations thereof); bicarbonates (e.g., LiHCO 3 , NaHCO 3 , KHCO 3 , and combinations thereof); and combinations thereof.
• the base can be in the form of a solid (e.g., crystals, granulates, and pellets); a liquid (e.g., an aqueous solution); and combinations thereof.
• the base has a pK b of 1 to 12, 1 to 10, 1 to 8, 1 to 6, 1 to 5, 2 to 12, 2 to 10, 2 to 8, 2 to 6, 2 to 5, 3 to 10, 3 to 6, 3 to 5, 4 to 10, 4 to 8, 4 to 6, 5 to 10, or 5 to 8.
• pK b refers to the negative logarithm of the base association constant, K b , of the base.
• K b refers to the equilibrium constant for the ionization of the base in water, wherein:
• a base is added in an amount of about 2% to about 10%, about 2% to about 9%, about 2% to about 8%, about 2% to about 7%, about 2% to about 6%, about 3% to about 6%, about 4% to about 6%, about 5% to about 6%, about 2% to about 5%, about 2% to about 4%, about 2% to about 3%, about 3% to about 5%, about 3% to about 4%, or about 4% to about 5% by weight (or volume) of the cell broth to raise the pH.
• the pH of the cells can be raised by a chloralkali process.
• the fermentation broth containing sodium chloride and the cells is subjected to electrolysis that results in the formation of sodium hydroxide, which raises the pH of the cell.
• the fermentation broth includes calcium chloride or potassium chloride instead of, or in addition to, sodium chloride, and electrolysis results in the formation of calcium hydroxide or potassium hydroxide, respectively, thereby raising the pH of the cell.
• the cells are lysed by lowering the pH of the cells.
• the pH is lowered by adding an acid.
• the acids include, but are not limited to, sulfuric; phosphoric; hydrochloric; hydrobromic; hydroiodic; hypochlorous; chlorous; chloric; perchloric; fluorosulfuric; nitric; fluoroantimonic; fluoroboric; hexafluorophosphoric; chromic; boric; acetic; citric; formic; and combinations thereof.
• Enzymatic treatment refers to contacting the cells with one or more enzymes.
• Enzymes include, but are not limited to, proteases, cellulases, hemicellulases, chitinases, pectinases, and combinations thereof.
• Non-limiting examples of proteases include serine proteases, theronine proteases, cysteine proteases, aspartate proteases, metalloproteases, glutamic acid proteases, alacase, and combinations thereof.
• Non-limiting examples of cellulases include sucrase, maltase, lactase, alpha-glucosidase, beta-glucosidase, amylase, lysozyme, neuraminidase, galactosidase, alpha-mannosidase, glucuronidase, hyaluronidase, pullulanase, glucocerebrosidase, galactosylceramidase, acetylgalactosaminidase, fucosidase, hexosaminidase, iduronidase, maltase-glucoamylase, and combinations thereof.
• a non-limiting example of a chitinase includes chitotriosidase.
• Non-limiting examples of pectinases include pectolyase, pectozyme, polygalacturonase, and combinations thereof.
• some enzymes are activated by heating.
• lysis does not include the use of enzymes.
• a “lysed cell composition” refers to a composition comprising one or more lysed cells, including cell debris and other contents of the cell, in combination with microbial oil (from the lysed cells), and optionally, a fermentation broth that contains liquid (e.g., water), nutrients, and microbial cells.
• a microbial cell is contained in a fermentation broth or media comprising water.
• a lysed cell composition refers to a composition comprising one or more lysed cells, cell debris, microbial oil, the natural contents of the cell, and aqueous components from a fermentation broth.
• the lysed cell composition comprises liquid, cell debris, and microbial oil.
• a lysed cell composition is in the form of an oil-in-water emulsion comprising a mixture of a continuous aqueous phase and a dispersed oil phase.
• a dispersed oil phase is present in a concentration of about 1% to about 60%; about 1% to about 50%; about 1% to about 40%; about 1% to about 30%; about 1% to about 20%; about 5% to about 60%; about 5% to about 50%; about 5% to about 40%; about 5% to about 30%; about 5% to about 20%; about 10% to about 60%; about 10% to about 50%; about 10% to about 40%; about 20% to about 60%; 20% to 50%, 20% to about 40%; about 30% to about 60%; about 30% to about 50%; or about 40% to about 60% by weight (or volume) of an emulsified lysed cell composition.
• lysing microbial cells results in the formation of an emulsion from endogenous materials in the cell or cell biomass including, but not limited to, proteins, phospholipids, carbohydrates, and combinations thereof.
• emulsion and emulsified refers to a mixture of two or more immiscible phases or layers wherein one phase or layer is dispersed in another phase or layer.
• break,” “break-up,” “demulsify,” “demulsification,” “demulsifying,” and “breaking” refer to a process of separating immiscible phases or layers of an emulsion.
• a process of the present invention breaks an oil-containing emulsion from a single-phase to two or more phases.
• the two or more phases include an oil phase and an aqueous phase.
• a process of the present invention breaks an oil-containing emulsion into at least three phases.
• the three phases are selected from an oil phase, an aqueous phase, and a solid phase.
• the phases are selected from an oil phase, an emulsion phase, an aqueous phase, and a solid phase.
• the mean particle size of the oil droplets formed during demulsification is selected from 5 microns to 50 microns; 5 microns to 45 microns; 5 microns to 40 microns; 5 microns to 35 microns; 5 microns to 30 microns; 5 microns to 25 microns; 5 microns to 20 microns; 5 microns to 15 microns; 10 microns to 50 microns; 10 microns to 45 microns; 10 microns to 40 microns; 10 microns to 35 microns; 10 microns to 30 microns; 10 microns to 25 microns; 10 microns to 20 microns; 10 microns to 15 microns; 15 microns to 50 microns; 15 microns to 45 microns; 15 microns to 40 microns; 15 microns to 35 microns; 15 microns to 30 microns; 15 microns to 25 microns; 15 microns to 20 microns; 15 microns to 50
• the mean particle size of the oil droplets formed during demulsification is selected from at least 10 microns, at least 15 microns, at least 20 microns, at least 25 microns, at least 30 microns, at least 35 microns, and at least 40 microns or above. In further embodiments, the mean particle size of the oil droplets formed during demulsification is selected from at least 10 microns, at least 15 microns, at least 20 microns, and at least 25 microns. In some embodiments, the mean particle size can be measured using, e.g., a Beckman Coulter LS 13 320 particle size analyzer (Beckman Coulter, Brea, Calif.). In some embodiments, the mean particle size can be measured using, e.g., a Malvern MS2000 particle size analyzer (Malvern Instruments Ltd., Worcestershire, United Kingdom).
• the emulsifier is a detergent. In some embodiments, the emulsifier is a surfactant. In some embodiments, the emulsifier is added prior to, during, or after lysis. In one embodiment, the emulsifier is added after lysis. In some embodiments, the emulsifier is added to the lysed cell composition.
• the term “emulsifier” refers to a substance that stabilizes an emulsion. Emulsifiers are selected from ionic emulsifiers, nonionic emulsifiers, and combinations thereof. In some embodiments, the emulsifier is an ionic emulsifier.
• the ionic emulsifier is selected from anionic emulsifiers, cationic emulsifiers, and combinations thereof.
• the anionic emulsifiers can be anionic sulfate emulsifiers, such as, for example, alkyl sulfates (e.g., ammonium lauryl sulfate, sodium lauryl sulfate (SLS)/sodium dodecyl sulfate (SDS), and combinations thereof), alkyl ether sulfates (e.g., sodium laureth sulfate/sodium lauryl ether sulfate, sodium myreth sulfate, and combinations thereof), and combinations thereof; anionic sulfonate emulsifiers, such as, for example, docusates (e.g., dioctyl sodium sulfosuccinate, sulfonate fluorosurfactants (
• the emulsifier is an anionic emulsifier.
• the anionic emulsifier is selected from an anionic sulfate emulsifier, an anionic sulfonate emulsifier, an anionic phosphate emulsifier, an anionic carboxylate emulsifier, and combinations thereof.
• an anionic emulsifier is an anionic sulfate emulsifier.
• an anionic sulfate emulsifier is selected from ammonium lauryl sulfate, sodium dodecyl sulfate, sodium laureth sulfate, sodium lauryl ether sulfate, sodium myreth sulfate, and combinations thereof.
• an anionic sulfate emulsifier is sodium dodecyl sulfate.
• the cationic emulsifier can be a pH-dependent primary amine; a pH-dependent secondary amine; a pH-dependent tertiary amine; octenidine dihydrochloride; a permanently charged quaternary ammonium cation (e.g., alkyltrimethylammonium salts (e.g., cetyl trimethylammonium bromide (CTAB)/hexadecyl trimethyl ammonium bromide, cetyl trimethylammonium chloride (CTAC), and combinations thereof), cetylpyridinium chloride (CPC), benzalkonium chloride (BAC), benzethonium chloride (BZT), 5-bromo-5-nitro-1,3-dioxane, dimethyldioctadecylammonium chloride, dioctadecyldimethylammonium bromide (DODAB), and combinations thereof); and combinations thereof.
• alkyltrimethylammonium salts
• the molecular weight of the emulsifier is selected from 500 g/mole or less, 450 g/mole or less, 400 g/mole or less, 350 g/mole or less, and 300 g/mole or less.
• the molecular weight of the emulsifier is selected from 250 g/mole to 500 g/mole, 250 g/mole to 450 g/mole, 250 g/mole to 400 g/mole, 250 g/mole to 350 g/mole, 250 g/mole to 300 g/mole, 300 g/mole to 500 g/mole, 300 g/mole to 450 g/mole, 300 g/mole to 400 g/mole, 300 g/mole to 350 g/mole, 350 g/mole to 500 g/mole, 350 g/mole to 450 g/mole, 350 g/mole to 400 g/mole, 400 g/mole to 500 g/mole, 400 g/mole to 450 g/mole, and 450 g/mole to 500 g/mole.
• the molecular weight of SDS is 288 g/mole
• the molecular weight of CTAB is 364 g/mole.
• the molecular weight of the emulsifier is selected from 250 g/mole to 450 g/mole, 250 g/mole to 400 g/mole, 250 g/mole to 350 g/mole, and 250 g/mole to 300 g/mole.
• an emulsifier is added as a powder. In some embodiments, an emulsifier is added in a solution having a concentration of emulsifier in an amount of 5% to 50%, 5% to 45%, 5% to 40%, 5% to 35%, 5% to 30%, 10% to 50%, 10% to 45%, 10% to 40%, 10% to 35%, 10% to 30%, 15% to 50%, 15% to 45%, 15% to 40%, 15% to 35%, 15% to 30%, 20% to 50%, 20% to 45%, 20% to 40%, 20% to 35%, 20% to 30%, 25% to 50%, 25% to 45%, 25% to 40%, 25% to 35%, 25% to 30%, 30% to 50%, 30% to 45%, 30% to 40%, and 30% to 35%.
• an emulsifier (e.g., in powder form or in solution) is added in an amount selected from 0.2% to 10%, 0.2% to 9.5%, 0.2% to 9%, 0.2% to 8.5%, 0.2% to 8%, 0.2% to 7.5%, 0.2% to 7%, 0.2% to 6.5%, 0.2% to 6%, 0.2% to 5.5%, 0.2% to 5%, 0.2% to 4.5%, 0.2% to 4%, 0.2% to 3.5%, 0.2% to 3%, 0.2% to 2.5%, 0.2% to 2%, 0.2% to 1.5%, 0.2% to 1%, 0.2% to 0.5%, 0.5% to 10%, 0.5% to 9.5%, 0.5% to 9%, 0.5% to 8.5%, 0.5% to 8%, 0.5% to 7.5%, 0.5% to 7%, 0.5% to 6.5%, 0.5% to 6%, 0.5% to 5.5%, 0.5% to 5%, 0.5% to 4.5%, 0.5% to 4%, 0.5% to 3.5%, 0.5% to 3%, 0.5% to 2.5%, 0.5% to 1.
• an emulsifier e.g., in powder form or in solution
• an emulsifier is added in an amount selected from 0.2% to 5%, 0.5% to 5%, 1% to 5%, 1.5% to 5%, 2% to 5%, 2.5% to 5%, and 3% to 5% by weight (or volume) of the cell broth or oil-containing emulsion.
• an emulsifier is added in an amount of from 0.2% to 10% by weight of the oil-containing emulsion.
• the emulsifier decreases the interfacial tension (i.e., surface tension) of the fermentation broth or lysed cell composition.
• interfacial tension or “surface tension” refers to the force which acts on an imaginary line one meter in length at the interface between two phases.
• the interfacial tension of the emulsion formed by the emulsifier is lower than an emulsion formed by the endogenous materials.
• the interfacial tension can be measured in dynes/cm.
• the emulsifier increases an absolute value of the zeta potential of the fermentation broth or lysed cell composition (i.e., increases a positive zeta potential or decreases a negative zeta potential).
• the addition of an anionic emulsifier can result in a downward shift in the zeta potential of the cell broth or oil-containing emulsion (e.g., decreases a positive zeta potential or increases a negative zeta potential).
• the addition of a cationic emulsifier can result in an upward shift in zeta potential of the cell broth or oil-containing emulsion (e.g., increases a positive zeta potential or increases a negative zeta potential).
• zeta potential refers to the electrokinetic potential between particles in the emulsion.
• the zeta potential can be measured in mV.
• the absolute value of the zeta potential of the emulsion formed by the emulsifier is higher than an emulsion formed by the endogenous materials.
• the addition of an ionic emulsifier creates an oil-in-water emulsion.
• the oil-in-water emulsion includes, but is not limited to, oil, water, and an ionic emulsifier.
• the process further comprises raising the pH of the coil-containing emulsion.
• the pH is raised by adding a base to the oil-containing emulsion.
• the bases that can be used to demulsify the oil-containing emulsion are the same as those set forth hereinabove.
• the pH is selected from about 7 or above; about 8 or above; about 9 or above; about 10 or above; about 11 or above; and about 12 or above.
• the pH is selected from a pH of 7 to 13; 7 to 12; 7 to 11; 7 to 10; 7 to 9; 8 to 13; 8 to 12; 8 to 11; 8 to 10; 8 to 9; 9 to 12; 9 to 11; 9 to 10; 10 to 12; and 10 to 11.
• the process further comprises adding a salt to the lysed cell composition.
• a salt refers to an ionic compound formed by replacing a hydrogen ion from an acid with a metal (e.g., an alkali metal, an alkali earth metal, and a transition metal) or a positively charged compound (e.g., NH 4 + ).
• the salt can be an alkali metal salt, alkali earth metal salts, sulfate salts, or combinations thereof.
• Negatively charged ionic species present in a salt include, but are not limited to, halides, sulfate, bisulfate, sulfite, phosphate, hydrogen phosphate, dihydrogen phosphate, carbonate, bicarbonate, and combinations thereof.
• a salt is selected from sodium chloride, sodium sulfate, sodium carbonate, calcium chloride, potassium sulfate, magnesium sulfate, monosodium glutamate, ammonium sulfate, potassium chloride, iron chloride, iron sulfate, aluminum sulfate, ammonium acetate, and combinations thereof.
• a salt does not include NaOH.
• a salt can be added as a solid (e.g., in crystalline, amorphous, pelletized, and/or granular form), and/or as a solution (e.g., a dilute solution, a saturated solution, or a super-saturated solution) containing, for example, water.
• a solution e.g., a dilute solution, a saturated solution, or a super-saturated solution
• the salt is added in an amount of 5 g/l to 25 g/l, 5 g/l to 10 g/l, 10 g/l to 15 g/l, 15 g/l to 20 g/l, 20 g/l to 25 g/l, or 10 g/l to 20 g/l.
• a salt is added to the lysed cell composition in an amount of 20% or less, 15% or less, 10% or less, 7.5% or less, 5% or less, or 2% or less by weight (or volume), of the lysed cell composition.
• a salt is added to the lysed cell composition in an amount of from about 0.05% to about 20%, about 0.1% to about 20%, about 0.1% to about 15%, about 0.1% to about 10%, about 0.5% to about 20%, about 0.5% to about 15%, about 0.5% to about 10%, about 0.5% to about 5%, about 0.5% to about 4%, about 0.5% to about 3%, about 0.5% to about 2.5%, about 0.5% to about 2%, about 0.5% to about 1.5%, about 0.5% to about 1%, about 1% to about 20%, about 1% to about 15%, about 1% to about 10%, about 1% to about 5%, about 1% to about 4%, 1% to about 3%, about 1% to about 2.5%, about 1% to about 2%, about 1% to about 1% to about
• a salt is added to the lysed cell composition in an amount of from about 0.05% to about 20%, about 0.1% to about 20% by weight (or volume), about 0.5% to about 15% by weight (or volume), or about 2% to about 10% by weight (or volume) of the cell broth.
• the process comprises heating the cells or the lysed cell composition to at least 10° C., at least 20° C., at least 25° C., at least 30° C., at least 35° C., at least 40° C., at least 45° C., at least 50° C., at least 55′′ C, at least 60° C., at least 65° C., at least 70° C., at least 75° C., at least 80° C., at least 85° C., at least 90° C., at least 95° C., or at least 100° C.
• the process comprises heating the lysed cell composition and/or cells to from about 10° C. to about 100° C., about 10° C.
• the process comprises heating the cells or the lysed cell composition from about 70° C. to about 100° C., about 70° C. to about 90° C., about 80° C. to about 100° C., about 80° C. to about 90° C., or about 90° C. to about 100° C.
• the process comprises heating the cells or the lysed cell composition from about 70° C. to about 100° C., about 70° C. to about 90° C., about 80° C. to about 100° C., about 80° C. to about 90° C., or about 90° C. to about 100° C.
• the process comprises heating the cells or the lysed cell composition from about 70° C. to about 100° C., about 70° C. to about 90° C., about 80° C. to about 100° C., about 80° C. to about 90° C., or about 90° C.
• the process comprises heating the cells or the lysed cell composition to at least 70° C., at least 75° C., at least 80° C., at least 85° C., at least 90° C., at least 95° C., or at least 100° C.
• cells and/or a lysed cell composition can be heated in a closed system or in a system with an evaporator. In some embodiments, cells and/or a lysed cell composition can be heated in a system with an evaporator such that a portion of the water present in the cells and/or the lysed cell composition is removed by evaporation. In some embodiments, the process comprises heating cells and/or a lysed cell composition in a system with an evaporator to remove up to 1%, 5%, 10%, 15%, 20%, 25%, 30%, 35%, 40%, 45% or 50% by weight (or volume) of water present in the cells and/or the lysed cell composition.
• the process comprises heating cells and/or a lysed cell composition in a system with an evaporator to remove 1% to 50%, 1% to 45%, 1% to 40%, 1% to 35%, 1% to 30%, 1% to 25%, 1% to 20%, 1% to 15%, 1% to 10%, 1% to 5%, 5% to 50%, 5% to 45%, 5% to 40%, 5% to 35%, 5% to 30%, 5% to 25%, 5° to 20%, 5% to 15%, 5% to 10%, 10% to 50%, 10% to 45%, 10% to 40%, 10% to 35%, 10% to 30%, 10% to 25%, 10% to 20%, 10% to 15%, 15% to 50%, 15% to 45%, 15% to 40%, 15% to 35%, 15% to 30%, 15% to 25%, 15% to 20%, 20% to 50%, 20% to 45%, 20% to 40%, 20% to 35%, 20% to 30%, 20% to 25%, 25% to 50%, 25% to 45%, 25% to 40%, 25% to 35%, 25% to 30%, 30% to 50%, 30% to 45%, 30% to 30% to 50%,
• agitating and “agitation” refer to a process of affecting motion in the cells and/or the lysed cell composition through an application of force.
• the process comprises agitating the cells and/or the lysed cell composition by stirring, mixing, blending, shaking, vibrating, or a combination thereof.
• the agitator is a dispersion style agitator that disperses a base and/or salt in the cells and/or the lysed cell composition.
• the agitator has a heating plate.
• the agitator has a mantle for stirring.
• an agitator has one or more impellers.
• impeller refers to a device arranged to impart motion to the cells or a lysed cell composition when rotated.
• Impellers suitable for use with the present invention include 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.
• the process of the invention comprises agitating the cells and/or the lysed cell composition at 0.1 hp/1,000 gal to 10 hp/1,000 gal, 0.5 hp/1,000 gal to 8 hp/1,000 gal, 1 hp/1,000 gal to 6 hp/1,000 gal, or 2 hp/1,000 gal to 5 hp/1,000 gal of composition.
• the process comprises agitating the cells and/or the lysed cell composition at 0.1 hp/1000 gal to 10 hp/1000 gal of composition.
• the invention comprises agitating at 10 rpm or below, 20 rpm or below, 50 rpm below, 100 rpm or below, 150 rpm or below, 200 rpm or below, 250 rpm or below, 300 rpm or below, 350 rpm or below, 400 rpm or below, 10 rpm to 400 rpm, 10 rpm to 350 rpm, 10 rpm to 300 rpm, 10 rpm to 250 rpm, 10 rpm to 200 rpm, 10 rpm to 150 rpm, 10 rpm to 100 rpm, 10 rpm to 50 rpm, 10 rpm to 20 rpm, 20 rpm to 400 rpm, 20 rpm to 350 rpm, 20 rpm to 300 rpm, 20 rpm to 250 rpm, 20 rpm to 200 rpm, 20 rpm to 150 rpm, 20 rpm to 100 rpm, 20 rpm to 50 rpm, 50 rpm to 100 r
• the process includes agitating cells and/or a lysed cell composition using an agitator having an impeller tip speed of 90 ft/min to 1,200 ft/min, 200 ft/min to 1,000 ft/min, 300 ft/min to 800 ft/min, 400 ft/min to 700 ft/min, or 500 ft/min to 600 ft/min.
• the process comprises agitating with an agitator having an impeller tip speed of 200 ft/min to 1000 ft/min.
• a process includes agitating cells and/or a lysed cell composition using an agitator having an impeller tip speed of 5 cm/sec to 900 cm/sec, 5 cm/sec to 750 cm/sec, 5 cm/sec to 500 cm/sec, 5 cm/sec to 350 cm/sec, 5 cm/sec to 300 cm/sec, 5 cm/sec to 250 cm/sec, 5 cm/sec to 200 cm/sec, 5 cm/sec to 150 cm/sec, 5 cm/sec to 100 cm/sec, 5 cm/sec to 50 cm/sec, 5 cm/sec to 25 cm/sec, 25 cm/sec to 900 cm/sec, 25 cm/sec to 750 cm/sec, 25 cm/sec to 500 cm/sec, 25 cm/sec to 350 cm/sec, 25 cm/sec to 300 cm/sec, 25 cm/sec to 250 cm/sec, 25 cm/sec to 200 cm/sec, 25 cm/sec to 150 cm/sec, 25 cm/sec to 100 cm/sec, 25 cm/sec to 50 cm/sec, 50 cm/sec to
• the agitating is performed in a container comprising an impeller, wherein a ratio of the impeller diameter to the container volume is 0.1 to 0.5, 0.1 to 0.4, 0.2 to 0.5, 0.2 to 0.4, 0.3 to 0.5, or 0.3 to 0.4.
• the agitating is performed in a container comprising an impeller, wherein a ratio of the impeller diameter to the inner diameter of the container is at least 0.25, at least 0.34, at least 0.65, 0.25 to 0.65, 0.25 to 0.33, 0.3 to 0.6, 0.3 to 0.5, 0.3 to 0.4, 0.34 to 0.65, 0.34 to 0.6, 0.34 to 0.55, 0.37 to 0.55, 0.4 to 0.65, 0.4 to 0.6, 0.4 to 0.5, or 0.42 to 0.55.
• agitating comprises mixing cells and/or a lysed cell composition such that the cells and/or the lysed cell composition is placed under flow conditions described by a Reynolds number of 10 to 10,000, 1,000 to 10,000, 1,500 to 10,000, or 2,000 to 10,000.
• a lysed cell emulsion during the agitating has a Reynolds number of 2,000 or more, 3,000 or more, or 5,000 or more, or 2,000 to 10,000, 3,000 to 10,000, or 5,000 to 10,000.
• the agitation vessels can have two impellers.
• the impellers are Rushton blade impellers.
• the impellers are separated from each other by a distance at least equal to a diameter of the smallest impeller.
• the impellers are 30 inches to 40 inches, 33 inches to 37 inches, 33 inches, 34 inches, 35 inches, 36 inches or 37 inches from tip to tip.
• the agitation vessels have a volume of at least 10,000 liters, at least 20,000 liters, at least 30,000 liters, at least 40,000 liters or at least 50,000 liters.
• the agitation vessels have an inner diameter of 90 inches to 110 inches, 95 inches to 105 inches, 98 inches, 99 inches, 100 inches, 101 inches, or 102 inches.
• a first impeller is located 15 inches to 20 inches, 16 inches to 19 inches, or 17 inches to 18 inches from a bottom of the agitation vessel and a second impeller is located 60 inches to 80 inches, 65 inches to 75 inches, 68 inches, 69 inches, 70 inches, 71 inches, 72 inches, 73 inches, 74 inches, or 75 inches above the first impeller.
• a lysed cell composition is agitated at least 50 rpm, at least 60 rpm, or at least 70 rpm.
• a lysed cell composition is agitated at 50 rpm to 70 rpm, 50 rpm to 60 rpm, or 60 rpm to 70 rpm.
• the process further comprises agitating the cells or lysed cell composition.
• the process comprises demulsifying an oil-containing emulsion and then separating the oil from the emulsion.
• the number of times the lysed cell composition is washed can be decreased by 1 time, 2 times, 3 times or more. In some embodiments, the washing is no more than 1 time, 2 times, or 3 times.
• the process can occur in a single vessel.
• the single vessel includes a fermentation vessel.
• the fermentation vessel can have a volume of at least 20,000 liters, at least 50,000 liters, at least 100,000 liters, at least 120,000 liters, at least 150,000 liters, at least 200,000 liters, or at least 220,000 liters.
• the fermentation vessel can have a volume of 20,000 liters to 220,000 liters, 20,000 liters to 100,000 liters, 20,000 liters to 50,000 liters, 50,000 liters to 220,000 liters, 50,000 liters to 150,000 liters, 50,000 liters to 100,000 liters, 100,000 liters to 220,000 liters, 100,000 liters to 150,000 liters, 100,000 liters to 120,000 liters, 150,000 liters to 220,000 liters, 150,000 liters to 200,000 liters, or 200,000 liters to 220,000 liters.
• a quantity of cells or a lysed cell composition formed in a vessel can be transferred into one or more agitation vessels.
• the agitation vessels can have a volume of at least 20,000 liters, at least 30,000 liters, at least 40,000 liters or at least 50,000 liters.
• the agitation vessels can have a volume of 20,000 liters to 50,000 liters, 20,000 liters to 40,000 liters, 20,000 liters to 30,000 liters, 30,000 liters to 50,000 liters, 30,000 liters to 40,000 liters or 40,000 liters to 50,000 liters.
• the processes described herein do not utilize an organic solvent to obtain, separate, or otherwise recover a microbial oil from the microbial cells.
• no organic solvent is used in obtaining microbial oil from microbial cells.
• an organic solvent is not added to cells, is not added to a lysed cell composition, and/or is not added to an oil during the processes disclosed herein in an amount or concentration sufficient to obtain a microbial oil.
• Organic solvents include polar solvents, non-polar solvents, water-miscible solvents, water-immiscible solvents, and combinations thereof.
• the process further comprises separating an oil-containing emulsion from a lysed cell composition.
• the process comprises separating an oil-containing emulsion from a lysed cell composition by heating the lysed cell composition.
• an oil is separated from a demulsified lysed cell composition by centrifuging the lysed cell composition.
• the separating comprises centrifuging at a temperature of 10° C. to 100° C.
• the oil-containing emulsion is separated from the lysed cell composition by first raising the pH (e.g. by adding a base that is described hereinabove) and then centrifuging the oil-containing emulsion and the lysed cell composition to obtain the oil-containing emulsion.
• the process comprises separating an oil-containing emulsion from the lysed cell composition by centrifuging the oil-containing emulsion and the lysed cell composition at a temperature of at least 10° C., at least 20° C., at least 25° C., at least 30° C., at least 35° C., at least 40° C., at least 45° C., at least 50° C., at least 55° C., at least 60° C., at least 65° C., at least 70° C., at least 75° C., at least 80° C., at least 85° C., at least 90° C., at least 95° C., or at least 100° C.
• the process comprises separating an oil-containing emulsion from the lysed cell composition by centrifuging the oil-containing emulsion and lysed cell composition at a temperature of 10° C. to 100° C., 10° C. to 90° C., 10° C. to 80° C., 20° C. to 100° C., 20° C. to 90° C., 20° C. to 80° C., 25° C. to 100° C., 25° C. to 90° C., 25° C. to 80° C., 25° C. to 75° C., 30° C. to 100° C., 30° C. to 90° C., 30° C. to 80° C., 40° C.
• centrifuging is conducted at a feed rate (of the lysed cell composition into a centrifuge) of 1 kilogram per minute (kg/min) to 500 kg/min, 1 kg/min to 400 kg/min, 1 kg/min to 300 kg/min, 1 kg/min to 200 kg/min, 1 kg/min to 100 kg/min, 1 kg/min to 75 kg/min, 1 kg/min to 50 kg/min, 1 kg/min to 40 kg/min, 1 kg/min to 30 kg/min, 1 kg/min to 25 kg/min, 1 kg/min to 10 kg/min, 10 kg/min to 500 kg/min, 10 kg/min to 400 kg/min, 10 kg/min to 300 kg/min, 10 kg/min to 200 kg/min, 10 kg/min to 100 kg/min, 10 kg/min to 75 kg/min, 10 kg/min to 50 kg/min, 10 kg/min to 40 kg/min, 10 kg/min to 30 kg/min, 20 kg/min to 500 kg/min, 20 kg/min to 400 kg/
• the process comprises centrifuging the lysed cell composition at a centrifugal force of 1,000 g to 25,000 g, 1,000 g to 20,000 g, 1,000 g to 10,000 g, 2,000 g to 25,000 g, 2,000 g to 20,000 g, 2,000 g to 15,000 g, 3,000 g to 25,000 g, 3,000 g to 20,000 g, 5,000 g to 25,000 g, 5,000 g to 20,000 g, 5,000 g to 15,000 g, 5,000 g to 10,000 g, 5,000 g to 8,000 g, 10,000 g to 25,000 g, 15,000 g to 25,000 g, or at least 1,000 g, at least 2,000, g, at least 4,000 g, at least 5,000 g, at least 7,000 g, at least 8,000 g, at least 10,000 g, at least 15,000 g, at least 20,000 g, or at least 25,000 g.
• the process comprises centrifuging a demulsified lysed cell composition at 4,000 rpm to 14,000 rpm, 4,000 rpm to 10,000 rpm, 6,000 rpm to 14,000 rpm, 6,000 rpm to 12,000 rpm, 8,000 to 14,000 rpm, 8,000 rpm to 12,000 rpm, or 8,000 rpm to 10,000 rpm.
• the oil can be recovered, for example, by decanting, skimming, vacuuming, pumping, sucking off, drawing off, siphoning, or otherwise recovering the microbial oil from the surface of the separated composition.
• the process comprises drying the oil that has been recovered to remove water from the oil.
• drying the oil can include, but is not limited to, heating the oil to evaporate water.
• the oil after drying, has a water content by weight (or volume) percentage of oil that is less than 3%, less than 2.5%, less than 2%, less than 1.5%, less than 1%, less than 0.5% less than 0.1%, or 0%.
• the oil after drying, has a water content by weight (or volume) percentage of oil of 0% to 3%, 0% to 2.5%, 0% to 2%, 0% to 1.5%, 0% to 1%, 0% to 0.5%, 0.1% to 3%, 0.1% to 2.5%, 0.1% to 2%, 0.1% to 1.5%, 0.1% to 1%, 0.1% to 0.5%, 0.5% to 3%, 0.5% to 2.5%, 0.5% to 2%, 0.5% to 1.5%, 0.5% to 1%, 1% to 3%, 1% to 2.5%, 1% to 2%, 1% to 1.5%, 1.5% to 3%, 1.5% to 2.5%, 1.5% to 2%, 2% to 3%, 2% to 2.5%, or 2.5% to 3%.
• a microbial oil that can be obtained from microbial cells by any of the processes disclosed herein.
• the oil comprises at least 30% by weight (or volume) arachidonic acid.
• the oil comprises at least 30% by weight (or volume) docoeahoxaenoic acid.
• the Anisidine value is determined in accordance with AOCS Official Method Cd 18-90.
• the oil described herein has an AV of less than about 50; less than about 40; less than about 30; less than about 20; less than about 15; or less than about 10.
• the oil has an AV of less than about 50.
• anisidine value refers to the measure of secondary reaction products, such as aldehydes and ketones that occur during oxidation of the oil.
• the peroxide value is determined in accordance with the AOCS Official Method Cd 8-53.
• the oil described herein has a PV less than about 20 meq/kg; less than about 10 meg/kg; or less than about 5 meg/kg. In some embodiments, the oil has a PV of less than about 5 meg/kg.
• peroxide value refers to the measure of primary reaction products, such as peroxides and hydroperoxides, that occur during oxidation of the oil. As used herein peroxide value is measured in meq/kg.
• the oil has a phosphorus content of 100 ppm or less, 95 ppm or less, 90 ppm or less, 85 ppm or less, 80 ppm or less, 75 ppm or less, 70 ppm or less, 65 ppm or less, 60 ppm or less, 55 ppm or less, 50 ppm or less, 45 ppm or less, 40 ppm or less, 35 ppm or less, 30 ppm or less, 25 ppm or less, 20 ppm or less, 15 ppm or less, 10 ppm or less, 9 ppm or less, 8 ppm or less, 7 ppm or less, 6 ppm or less, 5 ppm or less, 4 ppm or less, 3 ppm or less, 2 ppm or less, or 1 ppm or less. In some embodiments, the oil has a phosphorus content of about 8 ppm or less.
• the oil comprises one or more PUFAs. In some embodiments, the oil comprises at least 10%, at least 15%, at least 20%, at least 25%, at least 30%, at least 35%, at least 40%, at least 45%, at least 50%, at least 60%, at least 70% or at least 80% PUFA (by PUFA weight).
• the oil comprises at least 10%, at least 15%, at least 20%, at least 25%, at least 30%, at least 35%, at least 40%, at least 45%, at least 50%, at least 60%, at least 70% or at least 80% DHA (by DHA weight), and/or at least 10%, at least 15%, or at least 20% DPA n-6 (by DPA n-6 weight), and/or at least 10%, at least 15%, or at least 20% EPA (by EPA weight), and/or at least 10%, at least 15%, at least 20%, at least 25%, at least 30%, at least 35%, at least 40%, at least 45%, at least 50%, at least 55%, at least 60%, at least 65%, at least 70%, at least 75%, or at least 80% ARA (by ARA weight).
• an oil comprises less than 50%, less than 40%, less than 30%, less than 20%, less than 15%, less than 10%, or less than 5% EPA (by EPA weight). In some embodiments, an oil comprises less than 50%, less than 40%, less than 30%, less than 20%, less than 15%, less than 10%, or less than 5% DHA (by DHA weight). In some embodiments, an oil comprises less than 10%, less than 5%, less than 2%, less than 1%, or less than 0.5% by weight (or volume) sterols.
• an oil comprises at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, or 50% to 95%, 50% to 90%, 50% to 85%, 50% to 80%, 50% to 75%, 60% to 95%, 60% to 90%, 60% to 85%, 70% to 95%, 70% to 90%, 70% to 85%, 75% to 95%, 75% to 90%, or 75% to 85%, by weight (or volume) of triglycerides.
• the triglycerides comprise at least 10%, at least 20%, at least 30%, at least 35%, at least 40%, at least 50%, at least 60%, at least 70% or at least 80% by weight (or volume) DHA. In some embodiments, the triglycerides comprise at least 10%, at least 20%, at least 30%, at least 35%, at least 40%, at least 45%, at least 50%, at least 55%, at least 60%, at least 65%, at least 70%, at least 75%, or at least 80% by weight (or volume) ARA. In some embodiments, the triglycerides comprise at least 50%, at least 40%, at least 30%, at least 20%, at least 15%, at least 10%, or at least 5% by weight (or volume) EPA.
• the microbial oil obtained and/or recovered by any of the processes described herein is a crude oil.
• the oil described herein is a refined oil.
• a “crude oil” is an oil obtained from microbial cells without further processing.
• a “refined oil” is an oil obtained by treating a crude oil with standard processing of refining, bleaching, and/or deodorizing. See, e.g., U.S. Pat. No. 5,130,242.
• refining includes, but is not limited to, base refining, degumming, acid treatment, alkali treatment, cooling, heating, bleaching, deodorizing, deacidification, and combinations thereof.
• the process comprises concentrating a fermentation broth comprising microbial cells. In some embodiments, the process comprises concentrating the lysed cell composition.
• concentrating refers to removing water from a composition. Concentrating can include, but is not limited to, evaporating, chemical drying, centrifuging, and the like, and combinations thereof.
• a cell composition or a lysed cell composition is concentrated to provide an oil concentration of at least 4%, at least 5%, at least 10%, at least 15%, at least 20%, at least 25%, or at least 30% by weight (or volume) of the composition.
• a cell composition or a lysed cell composition is concentrated to provide an oil concentration of 4% to 40%, 4% to 30%, 4% to 20%, 4% to 15%, 5% to 40%, 5% to 30%, 5% to 20%, 10% to 40%, 10% to 30%, 10% to 20%, 15% to 40%, 15% to 30%, 20% to 40%, 20% to 30%, 25% to 40%, or 30% to 40% by weight (or volume) of the composition.
• Effective culture conditions for a microbial cell for use with the invention include, but are not limited to, effective media, bioreactor, temperature, pH, and oxygen conditions that permit oil production.
• An effective medium refers to any medium in which a microbial cell, e.g., Thraustochytriales microbial cell, is typically cultured.
• Such media typically comprises an aqueous medium having assimilable carbon, nitrogen, and phosphate sources, as well as appropriate salts, minerals, metals, and other nutrients, such as vitamins.
• Microbial cells for use with the present invention can be cultured in conventional fermentation bioreactors, shake flasks, test tubes, microtiter dishes, and petri plates.
• a microbial cell comprises at least 30% by weight (or volume) oil, at least 35% by weight (or volume) oil, at least 40% by weight (or volume) oil, at least 50% by weight (or volume) oil, at least 60% by weight (or volume) oil, at least 70% by weight (or volume) oil, or at least 80% by weight (or volume) oil.
• a microbial cell for use with the present invention is capable of producing at least 0.1 grams per liter per hour (g/L/h) of DHA, at least 0.2 g/L/h of DHA, at least 0.3 g/L/h of DHA, or at least 0.4 g/L/h of DHA.
• a microbial cell for use with the present invention is capable of producing at least 0.01 grams per liter per hour (g/L/h) of ARA, at least 0.05 g/L/h of ARA, at least 0.1 g/L/h of ARA, at least 0.2 g/L/h of ARA, at least 0.3 g/L/h of ARA, or at least 0.4 g/L/h of ARA.
• an oil obtained according to any of the processes described herein, the spent biomass, or combinations thereof can be used directly as a food or food ingredient, such as an ingredient in baby food, infant formula, beverages, sauces, dairy based foods (such as milk, yogurt, cheese and ice-cream), oils (e.g., cooking oils or salad dressings), and baked goods; nutritional supplements (e.g., in capsule or tablet forms); feed or feed supplement for any non-human animal (e.g., whose products (e.g., meat, milk, or eggs) are consumed by humans); food supplements; and pharmaceuticals (in direct or adjunct therapy application).
• a food or food ingredient such as an ingredient in baby food, infant formula, beverages, sauces, dairy based foods (such as milk, yogurt, cheese and ice-cream), oils (e.g., cooking oils or salad dressings), and baked goods
• nutritional supplements e.g., in capsule or tablet forms
• feed or feed supplement for any non-human animal e.g., whose products (e.g., meat, milk,
• animal refers to any organism belonging to the kingdom Animalia and includes any human animal, and non-human animal from which products (e.g., milk, eggs, poultry meat, beef, pork or lamb) are derived.
• the oil and/or biomass can be used in seafood. Seafood is derived from, without limitation, fish, shrimp and shellfish.
• products includes any product derived from such animals, including, without limitation, meat, eggs, milk or other products.
• the “extraction yield” is the amount, by weight, of lipid in the oil-containing emulsion expressed as a percentage of the amount, by weight, of lipid in the cell broth.
• the “refining yield” is the amount, by weight, of lipid in the refined oil expressed as a percentage of the amount, by weight, of lipid in the oil-containing emulsion.
• the “total yield” is the amount, by weight, of lipid in the refined oil expressed as a percentage of the amount, by weight, of lipid in the cell broth.
• An unwashed cell broth (75.9 kg) containing microbial cells ( Schizochytrium sp.) was pasteurized at 60° C. for 1 hour.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on the weight of the cell broth, agitated at a speed of 184 RPM, heated to 60° C. and held for 2 hours. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.5 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° f and held for 19 hours.
• the pH of the lysed cell composition was adjusted to 8.2 by adding 6N NaOH, agitated at 150 RPM, and held for 4.5 hours.
• the pH of the lysed cell composition was adjusted to 8.3 by adding 6N NaOH, agitated at 150 RPM, and held for 1 hour.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 87.2%.
• the recovered oil-containing emulsion had an AV of 12.3 and contained 1.24% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.2% by weight of the emulsion and held for 15 minutes.
• the oil-containing emulsion was further heated to 60-65° C. and NaOH was added in an amount of 12.5% by weight of the free fatty acid composition and weight of the oil-containing emulsion, and held for 30 minutes to refine the emulsion.
• the oil was separated from the emulsion by centrifuging.
• the refining yield was 86.2%.
• the total yield was 75%.
• the refined oil had an AV of 10.
• An unwashed cell broth (78.3 kg) containing microbial cells ( Schizochytrium sp.) was pasteurized at 60° C. for 1 hour.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the tell broth, agitated at a speed of 184 RPM, heated to 60° C. and held for 2 hours with pH controlled at 7.5 with 6N NaOH. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 9.7 by adding 6N NaOH.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.2% by weight of the emulsion and held for 15 minutes.
• the oil-containing emulsion was further heated to 60-65° C. and NaOH was added in an amount of 12.5% by weight of the free fatty acid composition and weight of the oil-containing emulsion, and held for 30 minutes to refine the emulsion.
• the oil was separated from the emulsion by centrifuging. The refining yield was 98.9%. The total yield was 85.3%.
• the recovered oil had an AV of 13.5 and contained 0.5% free fatty acids.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 185 RPM, heated to 60° C. and held for 2 hours with pH controlled at 7.5 with 6N NaOH. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 9.9 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C.
• the pH of the lysed cell composition was adjusted to 8.5 by adding 6N NaOH and held for 4 hours.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 94.4%.
• the oil-containing emulsion had an AV of 4.5 and contained 1.88% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C.
• the oil-containing emulsion was further heated to 60-65° C. and NaOH was added in an amount of 12.5% by weight of the free fatty acid composition and weight of the oil-containing emulsion, and held for 30 minutes to refine the emulsion.
• the oil was separated from the emulsion by centrifuging. The refining yield was 91.5%. The total yield was 86.4%.
• the refined oil had an AV of 13.5 and contained 0.5% free fatty acids.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 185 RPM, heated to 60° C. and held for 2 hours with pH controlled at 7.5 with 6N NaOH. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.2 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C.
• the oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 99.3%.
• the oil-containing emulsion had an AV of 4. and contained 0.67% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.2% by weight of the emulsion and held for 15 minutes.
• the oil-containing emulsion was further heated to 60-65° C. and NaOH was added in an amount of 12.5% by weight of the free fatty acid composition and weight of the oil-containing emulsion, and held for 30 minutes to refine the emulsion.
• the oil was separated from the emulsion by centrifuging.
• the refining yield was 92.7%.
• the total yield was 92.3%.
• the refined oil had an AV of 2.8 and contained 0.54% free fatty acids.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 183 RPM, heated to 60° C. and held for 2 hours with pH controlled at 7.5 with 6N NaOH. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.2 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed tell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 94%.
• the oil-containing emulsion contained 2.1% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.2% by weight of the emulsion and held for 15 minutes. The oil-containing emulsion was further heated to 60-65° C.
• the refined oil contained 0.62% free fatty acids.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 184 RPM, heated to 60° C. and held for 2 hours. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.5 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C. and held for 22 hours.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 93.9%.
• the oil-containing emulsion contained 1.5% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.2% by weight of the emulsion and held for 15 minutes. The oil-containing emulsion was further heated to 60-65° C.
• An unwashed cell broth (77.2 kg) containing microbial cells ( Schizochytrium sp.) was pasteurized at 60° C. for 1 hour. The cells were mechanically lysed. 6N NaOH was added to the lysed cell composition to pH adjust the composition to 9.5, NaCl in an amount of 2% by weight of the cell broth was added, agitated at 184 RPM, heated to 90° C. and held for 25 hours.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 91.1%.
• the oil-containing emulsion contained 1.7% free fatty acids.
• the oil-containing emulsion was heated to 50-55° C. and held for 8 hours and 15 minutes.
• the oil was separated from the emulsion by centrifuging.
• the refining yield was 83.7%.
• the total yield was 76.2%.
• An unwashed cell broth (74.8 kg) containing microbial cells ( Schizochytrium sp.) was pasteurized at 60° C. for 1 hour.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 184 RPM, heated to 60° C. and held for 2 hours. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.5 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C. and held for 23 hours.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 82.8%.
• the oil-containing emulsion contained 1.1% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.2% by weight of the emulsion and held for 15 minutes. The oil-containing emulsion was further heated to 60-65° C.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 184 RPM, heated to 60° C. and held for 2 hours. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.5 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C. and held for 22 hours.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 90.9%.
• the oil-containing emulsion contained 1.7% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.3% by weight of the emulsion and held for 15 minutes. The oil-containing emulsion was further heated to 60-65° C.
• the cells were lysed by adding 6N NaOH to pH adjust the broth to 7.5 and Alcalase® enzyme (available from Novozymes (Franklinton, N.C.)) was added in an amount of 0.5% based on weight of the cell broth, agitated at a speed of 185 RPM, heated to 60° C. and held for 2 hours with pH controlled at 7.5 with 6N NaOH. While maintaining the agitation, the pH of the lysed cell composition was adjusted to 10.5 by adding 6N NaOH. NaCl in an amount of 2% by weight of the cell broth was added and heated to 90° C.
• An oil-containing emulsion was formed and separated from the lysed cell composition by heating the oil-containing emulsion and lysed cell composition to 80° C. and then centrifuging (Alfa Laval Disc Stack Centrifuge, LAPX 404/Clara 20). The extraction yield was 96.9%.
• the oil-containing emulsion had an AV of 1.5, a PV of ⁇ 0.1 meg/kg and contained 0.87% free fatty acids.
• the oil-containing emulsion was placed in a 20 L tank with nitrogen blanketing and was heated to 50-55° C. and 50% citric acid was added in an amount of 0.3% by weight of the emulsion and held for 15 minutes.
• the oil-containing emulsion was further heated to 60-65° C. and NaOH was added in an amount of 12.5% by weight of the free fatty acid composition and weight of the oil-containing emulsion, and held for 30 minutes to refine the emulsion.
• the oil was separated from the emulsion by centrifuging. The total yield was 92.1%.
• the refined oil had an AV of 5.2, a PV of 0.52 meg/kg and contained 0.24% free fatty acids.
• Example 1 87.2% 20
• Example 2 86.3% 22.5
• Example 3 94.4% 22
• Example 4 99.3% 22
• Example 5 93.4% 22
• Example 6 93.9% 22
• Example 7 91.1% 25
• Example 8 82.8% 23
• Example 9 90.1% 22.6 Standard #1 91.3% 67 Standard #2 90.2% 43.5

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