WO2016092828A1 - 藻類の破砕方法 - Google Patents
藻類の破砕方法 Download PDFInfo
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- WO2016092828A1 WO2016092828A1 PCT/JP2015/006110 JP2015006110W WO2016092828A1 WO 2016092828 A1 WO2016092828 A1 WO 2016092828A1 JP 2015006110 W JP2015006110 W JP 2015006110W WO 2016092828 A1 WO2016092828 A1 WO 2016092828A1
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- heat treatment
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- 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
- C11B1/04—Pretreatment of vegetable raw material
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C19/00—Other disintegrating devices or methods
- B02C19/06—Jet mills
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- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C19/00—Other disintegrating devices or methods
- B02C19/06—Jet mills
- B02C19/065—Jet mills of the opposed-jet type
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B02—CRUSHING, PULVERISING, OR DISINTEGRATING; PREPARATORY TREATMENT OF GRAIN FOR MILLING
- B02C—CRUSHING, PULVERISING, OR DISINTEGRATING IN GENERAL; MILLING GRAIN
- B02C19/00—Other disintegrating devices or methods
- B02C19/06—Jet mills
- B02C19/066—Jet mills of the jet-anvil type
-
- 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
- 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
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- 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
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12N—MICROORGANISMS OR ENZYMES; COMPOSITIONS THEREOF; PROPAGATING, PRESERVING, OR MAINTAINING MICROORGANISMS; MUTATION OR GENETIC ENGINEERING; CULTURE MEDIA
- C12N1/00—Microorganisms, e.g. protozoa; Compositions thereof; Processes of propagating, maintaining or preserving microorganisms or compositions thereof; Processes of preparing or isolating a composition containing a microorganism; Culture media therefor
- C12N1/12—Unicellular algae; Culture media therefor
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- C—CHEMISTRY; METALLURGY
- C12—BIOCHEMISTRY; BEER; SPIRITS; WINE; VINEGAR; MICROBIOLOGY; ENZYMOLOGY; MUTATION OR GENETIC ENGINEERING
- C12P—FERMENTATION OR ENZYME-USING PROCESSES TO SYNTHESISE A DESIRED CHEMICAL COMPOUND OR COMPOSITION OR TO SEPARATE OPTICAL ISOMERS FROM A RACEMIC MIXTURE
- 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
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/10—Biofuels, e.g. bio-diesel
Definitions
- the present disclosure relates to a method for crushing algae and a method for extracting lipids from algae using the algae.
- Algae are known to produce lipids. If lipids produced by algae can be extracted efficiently, it can be an energy source to replace fossil fuels. In addition to energy sources, it can be a raw material for various products. However, when extracting lipids from algae, the cell wall is a major obstacle. In general, algae cell walls are hard and flexible and cannot be easily crushed. For this reason, it is not easy to efficiently recover products such as lipids from algae.
- Patent Document 1 discloses a method in which a non-polar solvent is brought into contact with a biomass suspension whose pH is adjusted, and a cell product is recovered from the non-polar solvent and the polar biomass solution. Is described.
- Patent Document 1 has a problem that the lipid yield is not sufficient. It is also shown that in order to obtain a high lipid yield, conditions of pH 1 and a processing temperature of 120 ° C. or higher are necessary. Therefore, very special equipment that can withstand strong acid conditions at high temperatures is required and it is extremely difficult to commercialize.
- the algae can be crushed efficiently, it is expected that the lipid yield from the algae can be greatly improved.
- the problem of the present disclosure is to enable efficient crushing of microalgae belonging to unequal hairy plants.
- One aspect of the method for crushing algae is that after heat-treating microalgae belonging to the hairless plant gate at a temperature of 40 ° C. or more and 65 ° C. or less under conditions of pH 3.5 or more and 9.5 or less, Physical processing is performed using a distributed device.
- the algal crushing method of the present disclosure it is possible to efficiently crush microalgae belonging to unequal plant gates.
- the microalgae belonging to the hairless plant gate refers to those belonging to the hairless plant gate among the microalgae.
- the microalgae refers to those having a cell size of 1 ⁇ m to 100 ⁇ m in the rest of the organisms that perform photosynthesis that generates oxygen, excluding moss plants, fern plants, and seed plants.
- the cell size is the major axis diameter of a cell measured with an optical microscope at an observation magnification of 400 times.
- Specific examples of the microalgae belonging to the trichomes include the Bacillariophyceae class and the Eustigmatophyceae class.
- microalgae of the class Bacillariophyceae include the genus Chaetoceros, the genus Nitzschia, the genus Skeletonema, and the like.
- microalgae of the Eustigmatophyceae class include the genus Nannochloropsis.
- Eustigmatophyceae class microalgae are preferable, and among them, the genus Nannochloropsis is more preferable.
- the algae belonging to the genus Nannochloropsis include Nannochloropsis oculata, Nannochloropsis salina, Nannochloropsis gaditana, and the like.
- the microalgae may be collected from swamps, ponds, etc., cultured, or commercially obtained.
- the algal crushing method of the present embodiment uses a high-pressure dispersion device after heat-treating microalgae belonging to the unequal hairy plant in a predetermined hydrogen ion concentration (pH) range within a predetermined temperature range. Do physical processing.
- the crushing method of the present embodiment can crush the algae in a state dispersed in a dispersion medium obtained by collection or culture. Moreover, you may process after performing operation, such as dilution or concentration for adjusting the density
- ⁇ Algae concentration is not particularly limited. From the viewpoint of improving productivity, algal crushability, and lipid recoverability, 0.5 g / L or more is preferable, 0.8 g / L or more is more preferable, 5 g / L or more is more preferable, and 10 g / L or more is preferable. Is even more preferable. In addition, from the viewpoints of algae crushability, lipid recovery and fluidity of the treatment liquid, it is preferably 200 g / L or less, more preferably 100 g / L or less, further preferably 50 g / L or less, and more preferably 30 g / L or less. More preferably, it is more preferably 20 g / L or less.
- the method for adjusting the concentration is not particularly limited.
- the concentration method include methods such as filtration, squeezing, centrifugation, gravity sedimentation, coagulation sedimentation, pressurized flotation, and evaporation of the dispersion medium.
- a flocculant such as aluminum sulfate
- the heat treatment and the physical treatment may be performed at different concentrations.
- the dilution method include a method of adding a liquid such as water.
- concentration of the micro algae in a process liquid is the value measured by the method described in the Example.
- the dispersion medium of the treatment liquid is not particularly limited as long as it can be in a predetermined pH range, but water is preferable from the viewpoint of economy.
- the water may be purified or may contain impurities. Moreover, seawater may be sufficient.
- the treatment liquid is an additive comprising one or more of a salt such as sodium chloride, a compound containing nitrogen or phosphorus, a trace metal, an inorganic flocculant, an organic flocculant, a chelating agent, and a buffer. May be included.
- a salt such as sodium chloride, a compound containing nitrogen or phosphorus, a trace metal, an inorganic flocculant, an organic flocculant, a chelating agent, and a buffer. May be included.
- the treatment solution may contain various components contained in a normal culture solution.
- water or an aqueous solution containing a predetermined additive can be used.
- the culture solution may be replaced with water or an aqueous solution containing a predetermined additive before treatment.
- the heat treatment is performed at a pH of 3.5 or higher, preferably 3.8 or higher, more preferably 4.0 or higher, still more preferably 4.5 or higher, even more preferably 5.0 or higher.
- the pH is 9.5 or less, preferably 9.0 or less, more preferably 8.5 or less, further preferably 8.0 or less, and even more preferably 7.5 or less. More preferably, it is 7.0 or less, More preferably, it is 6.5 or less, More preferably, it is 6.0 or less.
- the pH can be determined by measuring the pH of the treatment liquid at 25 ° C. by a measurement method according to JIS Z8802.
- the temperature of the heat treatment is 40 ° C. or higher, preferably 42 ° C. or higher, more preferably 43 ° C. or higher, more preferably 45 ° C. or higher, from the viewpoint of efficiently crushing microalgae. From the viewpoint of well crushing, it is 65 ° C. or less, preferably 62 ° C. or less, more preferably 60 ° C. or less, more preferably 57 ° C. or less, still more preferably 55 ° C. or less, even more preferably 52 ° C. or less, even more preferably. It is 50 degrees C or less.
- the heat treatment time represents the time during which the temperature of the treatment liquid is maintained within the temperature range of the heat treatment, and from the viewpoint of efficiently crushing microalgae, preferably 0.5 hours or more, more preferably 1 hour. Or more, more preferably 3 hours or more, even more preferably 5 hours or more, even more preferably 8 hours or more, even more preferably 10 hours or more, still more preferably 20 hours or more, even more preferably 24 hours or more, more More preferably, it can be 48 hours or more.
- the upper limit of the treatment time is preferably 96 hours or less, more preferably 72 hours or less, from the viewpoint of production efficiency.
- the heat treatment may be performed continuously for a predetermined time, but may be performed in a plurality of times so that the total is a predetermined time.
- the pH, temperature, and time can be freely combined within the above conditions, but from the viewpoint of efficiently crushing microalgae, the pH is 5.0 or more and 7.5 or less, and the temperature is 45 ° C or more. It is preferable that the temperature is 60 ° C. or less and the time is 10 hours or more.
- the heat treatment can be performed in an open or sealed treatment tank. What is necessary is just to control the temperature in a processing tank by a known method.
- a heat source and a control device that turns on and off the heat source so as to reach a predetermined temperature can be provided.
- the temperature control may be performed with the accuracy of normal industrial processing, and is preferably controlled to ⁇ 5 ° C. or less, more preferably ⁇ 3 ° C. or less, and further preferably ⁇ 1 ° C. or less. If control is difficult, the total time during which the temperature of the processing liquid is within the predetermined temperature range may be the predetermined time.
- the heat source may be provided inside or outside the processing tank.
- the treatment tank may be a batch type or a flow type. In the case of a flow type, it may be a passage-shaped treatment tank through which the treatment liquid flows.
- the heat treatment can be performed at normal pressure, but can also be performed in a pressurized or reduced pressure environment.
- the treatment temperature can be measured, for example, by inserting a thermometer or a temperature sensor into the treatment liquid. It is also possible to measure the liquid temperature of the processing liquid using a non-contact temperature sensor. Instead of directly measuring the temperature of the treatment liquid, the atmosphere temperature or the external temperature of the treatment tank may be measured. In this case, a correlation coefficient between the ambient temperature or the like and the temperature of the processing liquid may be obtained in advance, and the ambient temperature or the like may be converted into the temperature of the processing liquid. Further, by connecting the output of a thermometer or a temperature sensor to a recording device and recording the temperature continuously or periodically, it becomes possible to accurately manage the heat treatment time.
- the pH of the treatment liquid is not a predetermined value
- the pH can be adjusted by adding acid or alkali to the treatment liquid.
- the acid is not particularly limited, and an organic acid, a mineral acid, or a mixture thereof can be used.
- acetic acid, citric acid, phosphoric acid, hydrochloric acid, nitric acid or sulfuric acid can be used.
- the alkali is not particularly limited, and sodium carbonate, ammonia, sodium hydroxide, or the like can be used.
- the dispersion medium may be a buffer solution.
- the buffer solution may be selected according to the required pH, but a buffer solution containing acetic acid, citric acid, phosphoric acid, sodium carbonate, or the like can be used.
- any additive may be added to the treatment liquid during the heat treatment.
- an enzyme having a cell wall decomposing action such as hemicellulase, cellulase, pectinase, laminarinase and the like.
- a drug having an action of decomposing cell walls such as salt, alkali, surfactant, and detergent.
- these enzymes or chemicals may be contained in the treatment liquid.
- the physical treatment can be performed by a high-pressure dispersing device.
- the high-pressure disperser basically passes through a narrow flow path in a pressurized state with a treatment liquid containing dispersoids such as solid particles and droplet particles, and then suddenly depressurizes the solid particles and droplet particles. Is a device for further dispersing or pulverizing the dispersoid.
- the high-pressure dispersion device is also preferable from the viewpoint that mass processing is possible in industrialization.
- a high-pressure pump can be used for pressurizing the treatment liquid.
- the flow path having a narrow gap through which the processing liquid passes may have any structure as long as a predetermined pressure or the like can be applied.
- the value of the gap width or the like may be appropriately changed depending on the required pressure or the like.
- the flow path can be a straight pipe having a diameter of 1 ⁇ m to 2000 ⁇ m.
- an orifice having a hole of 1 ⁇ m to 2000 ⁇ m may be arranged in the middle of the straight pipe flow path. It is also possible to adopt a structure in which a slit having a gap of 1 ⁇ m to 2000 ⁇ m is disposed in the middle of the straight pipe flow path.
- the gap may be set to 1 ⁇ m to 2000 ⁇ m by forming a flow path in the gap between the valve tip and the valve receiver and adjusting the opening of the valve.
- the processing liquids may collide with each other by arranging the flow paths in the gap of 1 ⁇ m to 2000 ⁇ m to face each other.
- the treatment liquid may collide with the wall surface of the flow path by rapidly changing the flow path direction, for example, by bending the flow path at right angles.
- FIG. 1 shows an example of a homogeneous valve 100.
- the homogeneous valve 100 includes a homogeneous valve seat (valve receptacle) 101 in which a discharge hole is formed, a homogeneous valve main body 102 disposed at a position facing the discharge port of the homogeneous valve seat 101, and an impact ring surrounding the homogeneous valve main body 102. 103.
- a large pressure is applied to the processing liquid, and after passing through the gap, the pressure is rapidly reduced.
- the dispersoid in the processing liquid discharged from the discharge hole collides with the homogeneous valve main body 102 and the impact ring 103. Dispersoids are crushed by shear stress when passing through the gap, impact force due to impact, and cavitation due to pressure drop after passing through the gap.
- the shear force applied to the dispersoid can be adjusted by changing the size of the gap formed by the homogeneous valve seat 101, the homogeneous valve body 102, and the impact ring 103.
- the surface where the homogeneous valve seat 101 and the homogeneous valve body 102 face each other can be a smooth surface.
- a chamber type high-pressure dispersion device can be used for physical treatment.
- the chamber-type high-pressure dispersion device includes a type in which treatment liquids collide with each other or collide with a wall surface, and a type in which the processing liquids do not collide.
- a chamber-type high-pressure dispersion apparatus that collides treatment liquids has a chamber 110 as shown in FIG.
- a plurality of processing liquid inflow pipes 111, the same number of shear pipes 112 as the inflow pipes 111, and a single outflow pipe 113 are sequentially connected.
- the ends closer to the path 113 are connected at one place, and the treatment liquids collide with each other at the connection place.
- the dispersoid is crushed by shear stress in the shear pipe 112 that is narrower than the inflow pipe 111 and the outflow pipe 113, the impact force due to the collision between the processing liquids, and cavitation due to the pressure drop in the outflow pipe 113.
- a chamber-type high-pressure dispersion apparatus that collides a processing liquid with a wall surface has a chamber 120 as shown in FIG. 3, for example.
- a single liquid inflow conduit 121, a shear conduit 122, and an outflow conduit 123 are sequentially connected.
- the angle formed by the shear line 122 and the outflow line 123 is a right angle, and the liquid flow in the shear line 122 collides with the inner wall of the outflow line 123.
- the dispersoid is crushed by the shear stress in the shear pipe 122, the impact force caused by the collision between the treatment liquid and the wall surface, and the cavitation caused by the pressure drop in the outflow pipe 123.
- a chamber type high-pressure dispersion device that does not collide with the treatment liquid has a narrow shear line in the flow path, for example, and it is dispersed by shear stress in the shear line and cavitation due to pressure drop in the expanded outflow line. The quality is crushed.
- the pressure (inlet pressure) applied to the treatment liquid is 10 MPa or more in terms of gauge pressure from the viewpoint of efficiently crushing algae, preferably It is 30 MPa or more, more preferably 50 MPa or more, and further preferably 80 MPa or more. From the viewpoint of economy, it is preferably 200 MPa or less, more preferably 150 MPa or less, and further preferably 120 MPa or less. From the viewpoint of efficiently crushing algae and from the viewpoint of economy, the pressure (exit pressure) after the pressure reduction can be set to atmospheric pressure (0.1 MPa in absolute pressure).
- the outlet pressure is an absolute pressure, preferably 0.3 MPa or less, more preferably 0.2 MPa or less, still more preferably 0.15 MPa or less, even more Preferably it is 0.11 MPa or less.
- the homogeneous valve type high-pressure dispersion device examples include a pressure-type homogenizer (SMT Co., Ltd.), a high-pressure homogenizer (Izumi Food Machinery Co., Ltd.), and a minilab 8.3H type (Rannie).
- chamber-type high-pressure dispersers include microfluidizers (Microfluidics), Nanoveita (S.G. Company), Genus PY (Hakusui Chemical Co., Ltd.), DeBEE2000 (Nippon BB Co., Ltd.) and the like.
- a nano vater is preferable from the viewpoint that a small amount can be processed
- a pressure homogenizer is preferable from the viewpoint that a large amount can be processed in industrialization.
- the combination of heat treatment and physical treatment as described above can greatly improve the crushing efficiency over the case of physical treatment alone. it can.
- the temperature of the heat treatment is about 40 ° C. to 65 ° C. At such a temperature, the energy required for heat treatment for several hours to 10 hours is small, and the cost can be kept very low. For this reason, as compared with the case of physical processing alone, not only the crushing rate is improved, but also the substantial efficiency considering the required energy and cost is greatly improved.
- Physical treatment may be repeated multiple times after heat treatment. After the heat treatment, physical processing can be performed without performing other processing. Although the physical treatment can be performed immediately after the heat treatment, the physical treatment can be performed after the heat treatment is temporarily stored after the heat treatment. When storing the treatment liquid, it is preferably at a room temperature of about 15 to 25 ° C. from the viewpoint of reducing the required energy, and it is stored at a low temperature of about 5 to 15 ° C. from the viewpoint of suppressing lipid alteration. It is preferable to do. It can also be stored frozen. After the heat treatment, operations such as concentration of the treatment liquid, dilution or replacement of the dispersion medium, and pH adjustment of the treatment liquid can be performed before physical treatment.
- the crushing method of the present embodiment can be combined with a process for recovering lipid to extract a lipid.
- the higher the crushing rate the higher the yield of lipid from the microalgae treatment solution. Therefore, the yield of lipid can be greatly improved by crushing the microalgae belonging to the barrenaceous plant by extracting and recovering the lipid by the crushing method of the present embodiment that can efficiently crush. Further, by increasing the crushing rate in the crushing process, it is possible to obtain an advantage that the amount of the solvent used for extraction can be reduced and energy and cost required for the extraction can be reduced.
- lipids include simple lipids, complex lipids and derived lipids.
- Simple lipids include esters of fatty acids such as fats and oils or fatty acid esters and various alcohols.
- the complex lipid includes a phospholipid containing a fatty acid, alcohol and phosphoric acid, and a glycolipid containing a fatty acid, alcohol and sugar.
- Derived lipids are hydrolysis products of simple lipids or complex lipids, and include water-insoluble fatty acids, higher alcohols, sterols, terpenes, and fat-soluble vitamins. From the viewpoint of lipid recoverability, simple lipids or complex lipids are preferable, simple lipids are more preferable, and fats and oils are more preferable.
- Oils and fats mean esters of fatty acids and glycerin, specifically, neutral lipids such as monoglycerides, diglycerides, and triglycerides.
- the fatty acid which comprises fats and oils may not be single.
- the fatty acid may be any of short chain fatty acids having 2 to 4 carbon atoms, medium chain fatty acids having 5 to 12 carbon atoms, and long chain fatty acids having 12 or more carbon atoms.
- saturated fatty acid or unsaturated fatty acid may be sufficient.
- Specific examples of the saturated fatty acid include decanoic acid, dodecanoic acid, tetradecanoic acid, hexadecanoic acid, octadecanoic acid, and icosanoic acid.
- Specific examples of the monovalent unsaturated fatty acid include 9-hexadecenoic acid and 9-octadecenoic acid.
- polyunsaturated fatty acids include 9,12-octadecadienoic acid, 6,9,12-octadecatrienoic acid, 5,8,11,14-icosatetraenoic acid, 9,12,15-octa Examples include decatrienoic acid, 5,8,11,14,17-icosapentaenoic acid, and 4,7,10,13,16,19-docosahexaenoic acid.
- -Fatty acid ester- Fatty acid esters are esters of fatty acids and alcohols other than fats and oils, waxes that are esters of long-chain fatty acids and mono- or divalent higher alcohols, and esters of medium-chain fatty acids and lower or higher alcohols. Includes medium chain fatty acid esters and the like.
- the treatment for collecting the lipid is not particularly limited as long as the lipid can be separated from the treatment liquid containing the crushed fine algae.
- solvent extraction, centrifugation, stationary treatment, column chromatography and the like can be mentioned. These 1 type (s) or 2 or more types can be combined and applied.
- one or a combination of two or more selected from solvent extraction, centrifugation, and stationary treatment is preferable, and in particular, a combination of solvent extraction and centrifugation, or solvent extraction and stationary treatment. The combination with is preferable.
- Solvent extraction may be performed by adding an extraction solvent to the treatment solution after crushing microalgae. Stirring may be performed after adding the solvent. Since the lipid eluted from the microalgae is dissolved in the solvent, the lipid can be recovered by separating the solvent phase from the aqueous phase and recovering the solvent phase.
- solvent used for solvent extraction examples include esters such as methyl acetate and ethyl acetate; chain and cyclic ethers such as tetrahydrofuran and diethyl ether; polyethers such as polyethylene glycol; dichloromethane, chloroform, and tetrachloride.
- Halogenated hydrocarbons such as carbon; hydrocarbons such as hexane, cyclohexane, and petroleum ether; aromatic hydrocarbons such as benzene and toluene; pyridines; butanol, pentanol, hexanol, and isopropyl alcohol (2- Alcohols such as propanol); polyhydric alcohols such as butylene glycol; ketones such as methyl ethyl ketone; and supercritical carbon dioxide. These may be used alone or in combination of two or more.
- nonpolar solvents are preferred from the viewpoint of lipid recoverability.
- the nonpolar solvent include halogenated hydrocarbons, hydrocarbons, or aromatic hydrocarbons. Among them, hydrocarbons are preferable, and hexane is more preferable.
- a solvent compatible with water such as methanol, ethanol, propanol, ethylene glycol, propylene glycol, and acetone can be supplementarily added to the nonpolar solvent.
- supercritical extraction using supercritical carbon dioxide or the like can also be used. Further, dipping, decoction, leaching, reflux extraction, subcritical extraction, or the like can be used. For example, the method described in “Biochemical Experimental Method 24, Plant Lipid Metabolism Experimental Method” (edited by Akihiro Yamada, Society of Sciences Publishing Center, p. 3-4) can be referred to.
- the temperature for solvent extraction is not particularly limited, but is preferably 10 ° C. or higher, more preferably 20 ° C. or higher, from the viewpoint of lipid recovery. Further, from the viewpoints described above and economical viewpoints such as heating of the solvent, it is preferably 60 ° C. or lower, more preferably 50 ° C. or lower, and even more preferably 40 ° C. or lower.
- solvent extraction may be performed once or twice or more. When solvent extraction is performed twice or more, it may be performed with the same solvent or different solvents.
- Centrifugation can be performed using general equipment such as a separation plate type, a cylindrical type, or a decanter type.
- the centrifugal force in this case is preferably 500 G or more, more preferably 1000 G or more, from the viewpoint of lipid recoverability.
- Preferably it is 10,000 G or less, More preferably, it is 5000 G or less, More preferably, it can be 2000 G or less.
- the treatment time for the centrifugation is preferably 1 minute or more, more preferably 5 minutes or more, and even more preferably 10 minutes or more, from the viewpoint of lipid recoverability. Moreover, from an economical viewpoint, Preferably it is 80 minutes or less, More preferably, it is 40 minutes or less, More preferably, it can be 20 minutes or less.
- the temperature at the time of centrifugation is not particularly limited, but is preferably 10 ° C. or higher, more preferably 15 ° C. or higher, preferably 50 ° C. or lower, more preferably 40 ° C. or lower, from the viewpoint of lipid recovery and economy. It is.
- the solvent phase and aqueous phase can be separated quickly by centrifugation.
- reaction solution may be placed in a static state until the lipid and the aqueous phase are separated.
- solvent extraction it may be kept stationary until the solvent phase and the aqueous phase are separated.
- lipids can be extracted at a high recovery rate from microalgae that have accumulated lipids in the body by such a simple operation.
- Lipids extracted from microalgae can be used as biofuel such as biodiesel fuel directly or after being subjected to purification treatment or decomposition treatment. Further, it can be used as a raw material for functional foods or pharmaceuticals, a raw material for chemical products, and a raw material for cosmetics.
- the present disclosure further discloses a method for crushing the following algae and a method for extracting lipids from the algae.
- the pH is 3.5 or more, preferably 3.8 or more, more preferably 4.0 or more, still more preferably 4.5 or more, and even more preferably 5.0 or more, with respect to microalgae belonging to the trichomes. 9.5 or less, preferably 9.0 or less, more preferably 8.5 or less, even more preferably 8.0 or less, even more preferably 7.5 or less, even more preferably 7.0 or less, more More preferably 6.5 or less, still more preferably 6.0 or less, 40 ° C. or more, preferably 42 ° C. or more, more preferably 43 ° C. or more, more preferably 45 ° C. or more and 65 ° C. or less, preferably A temperature of 62 ° C.
- ⁇ 2> The method for disrupting algae according to ⁇ 1>, wherein the microalga is a genus Nannochloropsis.
- the heat treatment is preferably 0.5 hours or more, more preferably 1 hour or more, still more preferably 3 hours or more, still more preferably 5 hours or more, still more preferably 8 hours or more, even more preferably 10 hours or more,
- the algal crushing method according to ⁇ 1> or ⁇ 2> further preferably 20 hours or longer, more preferably 24 hours or longer, and even more preferably 48 hours or longer.
- ⁇ 4> The method for crushing algae according to any one of ⁇ 1> to ⁇ 3>, wherein the heat treatment is preferably 96 hours or less, more preferably 72 hours or less.
- the physical treatment is performed using the high-pressure dispersion apparatus, and preferably has a gauge pressure of 10 MPa or more, more preferably 30 MPa or more, still more preferably 50 MPa or more, still more preferably 80 MPa or more, preferably 200 MPa or less, more preferably 150 MPa or less, More preferably, after a pressure of 120 MPa or less is applied, the absolute pressure is preferably 0.3 MPa or less, more preferably 0.2 MPa or less, still more preferably 0.15 MPa or less, even more preferably 0.11 MPa or less, and even more.
- the method for disrupting algae according to any one of ⁇ 1> to ⁇ 4>, wherein the pressure is preferably reduced to atmospheric pressure (0.1 MPa).
- ⁇ 6> The method for disrupting algae according to any one of ⁇ 1> to ⁇ 5>, wherein the heat treatment is performed without intentional addition of an enzyme that degrades a cell wall.
- the heat treatment is performed at a temperature of 45 ° C. or higher and 60 ° C. or lower at a pH of 5.0 or higher and 7.5 or lower for 10 hours or longer, and any one of the above items ⁇ 1> to ⁇ 6>
- ⁇ 8> The algal crushing method according to any one of ⁇ 1> to ⁇ 7>, wherein the high-pressure dispersion apparatus is a homogeneous valve type high-pressure dispersion apparatus or a chamber type high-pressure dispersion apparatus.
- ⁇ 9> A method for extracting lipid from algae, wherein the lipid is recovered from a crushed alga obtained by the algae crushing method described in any one of ⁇ 1> to ⁇ 8>.
- the treatment for recovering the lipid is one or a combination of two or more selected from solvent extraction, centrifugation, stationary treatment, and column chromatography, preferably selected from solvent extraction, centrifugation, and stationary treatment.
- the lipid is extracted from the algae according to the above ⁇ 9>, which is a combination of one or more types, more preferably a combination of solvent extraction and centrifugation, or a combination of solvent extraction and stationary treatment Method.
- the solvent used for solvent extraction is preferably a nonpolar solvent, more preferably a hydrocarbon, and even more preferably hexane, and the lipid from the algae according to ⁇ 10>. How to extract.
- the temperature of solvent extraction is preferably 10 ° C. or higher, more preferably 20 ° C. or higher, preferably 60 ° C. or lower, more preferably 50 ° C. or lower, and even more preferably 40 ° C. or lower.
- the centrifugal force of centrifugation is preferably 500 G or more, more preferably 1000 G or more, preferably 10,000 G or less, more preferably 5000 G or less, and further preferably 2000 G or less, ⁇ 10 >
- the treatment time for centrifugation is preferably 1 minute or more, more preferably 5 minutes or more, further preferably 10 minutes or more, preferably 80 minutes or less, more preferably 40 minutes or less,
- the centrifugation treatment temperature is preferably 10 ° C. or higher, more preferably 15 ° C. or higher, preferably 50 ° C. or lower, more preferably 40 ° C. or lower.
- ⁇ Used alga body> Seawater samples containing algae were obtained from the coast near Ishigaki Island in Okinawa Prefecture. The obtained seawater sample was concentrated by a filter, and one algal cell strain was isolated by a micropipette. The isolated algal bodies were cultured in a culture solution (Daigo IMK medium, manufactured by Wako Pure Chemical Industries, Ltd.), and further the algal bodies were grown using the culture medium (f / 2 medium). A part of this alga body was requested to be analyzed by the University of Texas (UTEX Culture Collection) and identified as Nannochloropsis salina.
- Nannochloropsis oculata “Yanmarine K-1” manufactured by Chlorella Kogyo Co., Ltd., liquid constituting the treatment liquid: seawater, algal body concentration: 50 g / L was obtained and used in the experiment.
- the number of cells in 80 squares (16 squares ⁇ 5) of a 0.05 mm square block was counted.
- the depth of the calculation room of the bacteria counter is 0.020 mm, and the volume per block of 0.05 mm square is 1/20000 mm 3 .
- Daigo artificial seawater SP (made by Wako Pure Chemical Industries) was used for the dilution liquid.
- ⁇ Calculation of cell disruption rate The number of cells in the treatment solution was measured by the method for measuring the number of cells described above. The number of cells after the crushing treatment was subtracted from the number of cells before the crushing treatment, divided by the number of cells before the crushing treatment, and a value multiplied by 100 was taken as the cell crushing rate (%).
- the treatment liquid containing microalgae was centrifuged (15000 rpm, 5 minutes, 25 ° C.) with a centrifuge (manufactured by HITACHI, CR22GIII, rotor: 18A), the supernatant was discarded, and 0.125 M citric acid ⁇ Redispersed in disodium hydrogen phosphate buffer (pH 5).
- the redispersed liquid was suction filtered with a filter (Nihon Pole, Supor-450, pore size 0.45 ⁇ m) and washed with an equal amount of distilled water.
- the filter in which the algal bodies were collected was transferred to an aluminum cup and dried at 105 ° C. for 2 hours.
- the weight after drying was measured, and the tare of the filter was subtracted to obtain the algal body concentration (g / L). Also, if the treatment liquid is difficult to filter by suction with a filter, dilute the treatment liquid to an appropriate concentration, measure the weight after drying, subtract the tare of the filter, and then multiply by the dilution factor to obtain the algal body concentration ( g / L). In addition, 0.125M citrate-disodium hydrogen phosphate buffer (pH 5) can be used as the diluent.
- a treatment liquid containing a predetermined concentration of microalgae was placed in a polyethylene container and allowed to stand in a chamber of a vacuum dryer (manufactured by Yamato Kagaku Co., ADP300) set at a predetermined temperature in advance. The inside of the chamber was atmospheric pressure. After a predetermined time had elapsed, the sample was removed from the dryer and cooled at room temperature. In addition, when processing at 25 degreeC as a comparison, the temperature of the laboratory was set to 25 degreeC and the sample was left still in the laboratory. As a comparison, when processing at 4 ° C., the sample was left in a refrigerator (MPR-1411, manufactured by Sanyo Electric Co., Ltd.). After a predetermined time, the sample was removed from the refrigerator and returned to room temperature.
- a vacuum dryer manufactured by Yamato Kagaku Co., ADP300
- the physical treatment was performed with a high-pressure dispersing device.
- a high-pressure dispersion device Nanovater “NM2-L200-D” (manufactured by Yoshida Kikai Kogyo Co., Ltd., cross-type nozzle: NVGL-XT160) or pressure homogenizer “LAB2000” (manufactured by SMT Co., Ltd.) was used.
- the treatment pressure was 100 MPa as the inlet pressure and 0.1 Mpa (atmospheric pressure) as the absolute outlet pressure, and was obtained from the seventh shot for cutting off. The number of passes was one.
- the treatment pressure was 100 MPa (gauge pressure) as the inlet pressure and 0.1 MPa (atmospheric pressure) as the absolute pressure as the outlet pressure.
- the 300 cc processing liquid after the start of processing was discarded for cutting off, and a processing sample was obtained from 300 cc and thereafter. The number of passes was one.
- lipid content in dry algae was analyzed according to the method for extracting lipids from biomaterials (Bligh & Dyer method) reported in 1959 by EGBligh and WJDyer (EGBligh, WJDyer, Canadian journal of biochemistry and physiology, 37 (1959 ), P.911-917).
- This chloroform / methanol solvent extraction method is effective for simply measuring the amount of lipid in algal cells, but from the viewpoint of the safety, recoverability, and recyclability of the solvent used, it is not suitable for industrial practical use. This is not a suitable method.
- Lipids were recovered by solvent extraction as shown below. The collected lipid was converted to methyl ester, and the amount of lipid was quantified by the above-mentioned GC.
- Lipid recovery rate (%) lipid amount in hexane / lipid amount in dry alga body ⁇ 100 (1)
- Nannochloropsis salina (Liquid constituting treatment liquid: artificial seawater (Daigo artificial seawater SP, manufactured by Nippon Pharmaceutical Co., Ltd., alga body concentration: 1.0 g / L) ) was used.
- the pH of the treatment liquid at 25 ° C. was 7.3.
- 1M HCl was added dropwise to adjust the pH of the treatment solution to 5.0.
- the solution whose pH was adjusted was heat-treated.
- the treatment temperature was 50 ° C. and the treatment time was 1 hour.
- the physical treatment was performed using a nano perennial under the condition where the inlet pressure was 100 MPa.
- the cell disruption rate was 38.6%.
- Example 2 Example 1 was repeated except that the heat treatment time was 2 hours. The cell disruption rate was 33.9%.
- Example 3 Example 1 was repeated except that the heat treatment time was 3 hours. The cell disruption rate was 45.8%.
- Example 4 Example 1 was repeated except that the heat treatment time was 5 hours. The cell disruption rate was 47.4%.
- Example 5 Example 1 was repeated except that the heat treatment time was 10 hours. The cell disruption rate was 60.5%.
- Example 6 Example 1 was repeated except that the heat treatment time was 24 hours. The cell disruption rate was 87.0%. Moreover, the lipid recovery rate after crushing was 69%.
- Example 7 The same procedure as in Example 6 was performed except that the inlet pressure in the physical treatment was 50 MPa. The cell disruption rate was 75.9%. Moreover, the lipid recovery rate after crushing was 70%.
- Example 1 Example 1 was repeated except that the pH was not adjusted and no heat treatment was performed. That is, after obtaining a treatment liquid of Nannochloropsis salina (liquid constituting the treatment liquid: artificial seawater (Daigo Artificial Seawater SP, manufactured by Nippon Pharmaceutical Co., Ltd., alga body concentration: 1.0 g / L)) With the pH of 7.3, physical treatment was performed with a high-pressure disperser Nanovaita within 30 minutes after the sample was obtained, with the inlet pressure being 100 MPa. The cell disruption rate was 16.9%.
- Nannochloropsis salina liquid constituting the treatment liquid: artificial seawater (Daigo Artificial Seawater SP, manufactured by Nippon Pharmaceutical Co., Ltd., alga body concentration: 1.0 g / L)
- Example 2 Example 1 was repeated except that no heat treatment was performed. That is, the treatment liquid of Nannochloropsis salina (Nannochloropsis salina) (liquid constituting the treatment liquid: artificial seawater (Daigo Artificial Seawater SP, manufactured by Nippon Pharmaceutical Co., Ltd., alga body concentration: 1.0 g / L)) After adjusting the pH to 5.0 at 25 ° C. using HCl, physical treatment was performed under a condition of an inlet pressure of 100 MPa using a high-pressure dispersion apparatus Nano perenniala without performing heat treatment within 30 minutes. The cell disruption rate was 18.7%. Moreover, the lipid recovery rate after crushing was 6%.
- Example 3 (Comparative Example 3) Example 1 was repeated except that the heat treatment temperature was 25 ° C. The cell disruption rate was 16.1%.
- Example 4 (Comparative Example 4) Example 1 was repeated except that the heat treatment temperature was 25 ° C. and the heat treatment time was 2 hours. The cell disruption rate was 11.9%.
- Example 1 (Comparative Example 5) Example 1 was repeated except that the heat treatment temperature was 25 ° C. and the heat treatment time was 3 hours. The cell disruption rate was 13.2%.
- Example 1 (Comparative Example 6) Example 1 was repeated except that the heat treatment temperature was 25 ° C. and the heat treatment time was 10 hours. The cell disruption rate was 18.5%.
- Example 7 Example 1 was repeated except that the heat treatment temperature was 25 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 16.1%.
- Example 1 was repeated except that the heat treatment temperature was 80 ° C. The cell disruption rate was 21.8%.
- Example 1 was repeated except that the heat treatment temperature was 80 ° C. and the heat treatment time was 2 hours. The cell disruption rate was 18.5%.
- Example 1 (Comparative Example 10) Example 1 was repeated except that the heat treatment temperature was 80 ° C. and the heat treatment time was 3 hours. The cell disruption rate was 24.8%.
- Example 1 was repeated except that the heat treatment temperature was 80 ° C. and the heat treatment time was 10 hours. The cell disruption rate was 18.5%.
- Example 1 was repeated except that the heat treatment temperature was 80 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 23.0%.
- Comparative Example 13 After crushing as in Comparative Example 2, heat treatment was performed at 50 ° C. for 24 hours. The cell disruption rate was 19.3%.
- Example 8 Example 1 was repeated except that the heat treatment temperature was 40 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 49.5%. Moreover, the lipid recovery rate after crushing was 33%.
- Example 9 Example 1 was repeated except that the heat treatment temperature was 45 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 92.0%. Moreover, the lipid recovery rate after crushing was 74%.
- Example 10 Example 1 was repeated except that the heat treatment temperature was 55 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 81.2%. Moreover, the lipid recovery rate after crushing was 73%.
- Example 11 Example 1 was repeated except that the heat treatment temperature was 60 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 72.1%. Moreover, the lipid recovery rate after crushing was 55%.
- Example 1 was repeated except that the heat treatment temperature was 4 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 19.9%.
- Example 1 was repeated except that the heat treatment temperature was 37 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 19.0%.
- Example 1 was repeated except that the heat treatment temperature was 70 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 29.4%.
- Example 1 was repeated except that the heat treatment temperature was 80 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 23.0%.
- Example 12 The same procedure as in Example 1 was performed except that the pH of the treatment solution was adjusted to 4.0 at 25 ° C. using 1 M HCl and the heat treatment time was 10 hours. The cell disruption rate was 40.3%.
- Example 13 Example 12 was repeated except that the heat treatment time was 24 hours. The cell disruption rate was 66.0%.
- Example 14 The process was the same as Example 1 except that the pH of the treatment liquid was adjusted to 6.8 at 25 ° C. and the heat treatment time was 24 hours. The cell disruption rate was 53.5%.
- Example 15 The procedure was the same as Example 1 except that the pH of the treatment liquid was not adjusted, the pH at 25 ° C. was kept at 7.3, and the heat treatment time was 24 hours. The cell disruption rate was 52.3%.
- Example 16 Example 15 was repeated except that the heat treatment time was 48 hours. The cell disruption rate was 66.6%.
- Example 17 The procedure was the same as Example 1 except that the pH of the treatment solution was adjusted to 9.0 at 25 ° C. using 1 M NaOH and the heat treatment time was 24 hours. The cell disruption rate was 47.4%.
- Example 18 The procedure was the same as Example 1 except that the pH of the treatment solution was adjusted to 2.0 at 25 ° C. with 1M HCl and the heat treatment time was 24 hours. The cell disruption rate was 23.6%.
- Example 19 The process was performed in the same manner as in Example 1 except that the pH of the treatment solution was adjusted to 3.0 at 25 ° C. with 1 M HCl and the heat treatment time was 24 hours. The cell disruption rate was 16.0%.
- Example 20 The procedure was the same as Example 1 except that the pH of the treatment solution was adjusted to 10.0 at 25 ° C. with 1 M NaOH and the heat treatment time was 24 hours. The cell disruption rate was 26.5%.
- Example 21 The treatment solution was adjusted to 12.0 at 25 ° C. with 1 M NaOH, and the same treatment as in Example 1 was conducted except that the heat treatment time was 24 hours. The cell disruption rate was 18.6%.
- Table 4 summarizes the working conditions and cell disruption rates for Examples 12 to 17 and Comparative Examples 18 to 21.
- Example 18 Nannochloropsis oculata "Chilled Nanno Yanmarine K-1" (manufactured by Chlorella Kogyo Co., Ltd., liquid constituting seawater, alga body concentration: 50 g / L) It was used after returning to room temperature. Furthermore, this processing liquid was diluted with artificial seawater (manufactured by Nippon Pharmaceutical Co., Ltd., Daigo artificial seawater SP for marine microalgae) to adjust the algal body concentration to 1.0 g / L. The pH of the treatment liquid at 25 ° C. was 5.0. The same treatment as in Example 1 was performed except that the heat treatment time was changed to 5 hours using the above treatment liquid. The cell disruption rate was 47.4%.
- Example 19 Example 18 was repeated except that the heat treatment time was 10 hours. The cell disruption rate was 49.4%.
- Example 22 The procedure was the same as Example 18 except that the pH was not adjusted and no heat treatment was performed.
- the treatment solution of Nannochloropsis oculata “Refrigerated Nanno Yanmarine K-1” (algae concentration: 1.0 g / L) was heat-treated within 30 minutes after dilution while maintaining the pH at 25 ° C. at 6.8. Instead, physical treatment was performed in a high-pressure dispersion apparatus. The cell disruption rate was 19.6%.
- Example 18 was the same as Example 18 except that the heat treatment temperature was 25 ° C. and the heat treatment time was 10 hours. The cell disruption rate was 22.7%.
- Table 5 summarizes the working conditions and cell disruption rates for Examples 18 to 19 and Comparative Examples 22 to 23.
- Nannochloropsis salina Liquid constituting treatment liquid: artificial seawater (Daigo artificial seawater SP, manufactured by Nippon Pharmaceutical Co., Ltd., alga body concentration: 1.0 g / L) )
- the pH of the treatment liquid was 7.3.
- aluminum sulfate manufactured by Central Glass Co., Ltd., trade name “sulfuric acid band” is added to the treatment liquid. It added so that it might become 0.1%, and stirred for 5 minutes. Then, stirring was stopped and it left still at room temperature for 3 hours.
- the algal bodies aggregated and settled. Thereafter, a part of the supernatant was discarded to adjust the algal cell concentration to 15.2 g / L. 1M HCl was added dropwise, and the pH of the treatment solution was adjusted to 5.0 at 25 ° C. The solution whose pH was adjusted was heat-treated. The treatment temperature was 50 ° C. and the treatment time was 24 hours. After the heat treatment, physical treatment was performed using a pressure homogenizer under the condition of an inlet pressure of 100 MPa. The cell disruption rate was 77.6%.
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Abstract
Description
本開示において、不等毛植物門に属する微細藻類とは、微細藻類のうち、不等毛植物門に属するものをいう。微細藻類とは、酸素を発生する光合成を行う生物の中からコケ植物、シダ植物、及び種子植物を除いた残りのうちの、細胞サイズが直径1μm~100μmのものをいう。なお、細胞サイズは、光学顕微鏡を用いて観察倍率400倍で測定した細胞の長軸径である。不等毛植物門に属する微細藻類の具体例としてはBacillariophyceae綱、及びEustigmatophyceae綱等が挙げられる。Bacillariophyceae綱の微細藻類の具体例としては、Chaetoceros属、Nitzschia属、及びSkeletonema属等が挙げられる。Eustigmatophyceae綱の微細藻類の具体例としては、Nannochloropsis(ナンノクロロプシス)属が挙げられる。このうち、脂質の生産性及び脂質の回収性の観点から、Eustigmatophyceae綱の微細藻類が好ましく、中でもNannochloropsis属がより好ましい。Nannochloropsis属の藻類としては、Nannochloropsis oculata、Nannochloropsis salina、Nannochloropsis gaditanaなどが例示される。微細藻類は、沼や池等に生息するものを採取したものでも、培養したものでもよく、さらには商業的に入手したものでもよい。
本実施形態の藻類の破砕方法は、不等毛植物門に属する微細藻類に対して、所定の水素イオン濃度(pH)範囲で、所定温度範囲にて熱処理をした後、高圧分散装置を用いて物理的処理をする。
・pH
熱処理は、微細藻類を効率良く破砕する観点から、pH3.5以上、好ましくは3.8以上、より好ましくは4.0以上、さらに好ましくは4.5以上、よりさらに好ましくは5.0以上であり、そして、微細藻類を効率良く破砕する観点から、pH9.5以下、好ましくは9.0以下、より好ましくは8.5以下、さらに好ましくは8.0以下、よりさらに好ましくは7.5以下、よりさらに好ましくは7.0以下、よりさらに好ましくは6.5以下、よりさらに好ましくは6.0以下である。
熱処理の温度は、微細藻類を効率良く破砕する観点から、40℃以上、好ましくは42℃以上、より好ましくは43℃以上、さらに好ましくは45℃以上であり、そして、微細藻類を効率良く破砕する観点から、65℃以下、好ましくは62℃以下、より好ましくは60℃以下、さらに好ましくは57℃以下、よりさらに好ましくは55℃以下、よりさらに好ましくは52℃以下、よりさらに好ましくは50℃以下である。
熱処理の時間は、処理液の温度を上記の熱処理の温度範囲内で維持した時間を表し、微細藻類を効率良く破砕する観点から、好ましくは0.5時間以上、より好ましくは1時間以上、さらに好ましくは3時間以上、よりさらに好ましくは5時間以上、よりさらに好ましくは8時間以上、よりさらに好ましくは10時間以上、よりさらに好ましくは20時間以上、よりさらに好ましくは24時間以上、よりさらに好ましくは48時間以上とすることができる。処理時間の上限は、生産効率の観点から、好ましくは96時間以下、より好ましくは72時間以下とすることができる。
物理的処理は、高圧分散装置により行うことができる。高圧分散装置は、基本的に、固体粒子や液滴粒子等の分散質を含む処理液を加圧した状態で狭い流路を通過させ、その後急激に減圧することで固体粒子や液滴粒子等の分散質をさらに分散又は粉砕する装置である。高圧分散装置は、工業化において大量処理が可能であるという観点からも好ましい。
本実施形態の破砕方法は、脂質を回収する処理と組み合わせて、脂質を抽出する方法とすることができる。破砕率が高いほど、微細藻類の処理液からの脂質の収率が向上する。従って、効率良く破砕できる本実施形態の破砕方法により、不等毛植物門に属する微細藻類を破砕してから脂質を抽出して回収することにより、脂質の収率を大きく向上することができる。また、破砕処理における破砕率を高くすることにより、抽出に用いる溶媒の量を低減できたり、抽出に必要とするエネルギーや費用を低減できたりするという利点も得られる。
本開示において、脂質には、単純脂質、複合脂質及び誘導脂質が含まれる。単純脂質には、油脂又は脂肪酸エステルなどの脂肪酸と各種アルコールとのエステル等が含まれる。複合脂質には、脂肪酸、アルコール及びリン酸を含むリン脂質、並びに脂肪酸、アルコール及び糖を含む糖脂質等が含まれる。誘導脂質には、単純脂質又は複合脂質の加水分解生成物であり、水に不溶性の脂肪酸、高級アルコール、ステロール、テルペン、及び脂溶性ビタミン等が含まれる。脂質の回収性の観点から、単純脂質又は複合脂質が好ましく、単純脂質がより好ましく、油脂がさらに好ましい。
油脂とは、脂肪酸とグリセリンとのエステルを意味し、具体的には、モノグリセリド、ジグリセリド、及びトリグリセリドのような中性脂質をいう。油脂を構成する脂肪酸は、単一でなくてよい。
脂肪酸は、炭素数が2~4の短鎖脂肪酸、炭素数が5~12の中鎖脂肪酸、及び炭素数が12以上の長鎖脂肪酸のいずれであってもよい。また、飽和脂肪酸でも不飽和脂肪酸でもよい。飽和脂肪酸の具体例としては、デカン酸、ドデカン酸、テトラデカン酸、ヘキサデカン酸、オクタデカン酸、及びイコサン酸が挙げられる。一価の不飽和脂肪酸の具体例としては、9-ヘキサデセン酸、及び9-オクタデセン酸等が挙げられる。多価の不飽和脂肪酸の具体例としては、9,12-オクタデカジエン酸、6,9,12-オクタデカトリエン酸、5,8,11,14-イコサテトラエン酸、9,12,15-オクタデカトリエン酸、5,8,11,14,17-イコサペンタエン酸、及び4,7,10,13,16,19-ドコサヘキサエン酸が挙げられる。
脂肪酸エステルとは、油脂以外の、脂肪酸とアルコールとのエステルであり、長鎖脂肪酸と1価又は2価の高級アルコールとのエステルである蝋、中鎖脂肪酸と低級又は高級アルコールとのエステルである中鎖脂肪酸エステル等を含む。
脂質を回収する処理は、微細藻類の破砕物を含む処理液から脂質を分取することができれば特に限定されない。例えば、溶媒抽出、遠心分離、静置処理、カラムクロマトグラフィー等が挙げられる。これらの1種又は2種以上を組み合わせて適用することができる。中でも、脂質の回収性の観点から、溶媒抽出、遠心分離及び静置処理から選ばれる1種又は2種以上の組み合わせが好ましく、中でも溶媒抽出と遠心分離との組み合わせ、又は溶媒抽出と静置処理との組み合わせが好ましい。
不等毛植物門に属する微細藻類に対し、pHが3.5以上、好ましくは3.8以上、より好ましくは4.0以上、さらに好ましくは4.5以上、よりさらに好ましくは5.0以上であり、9.5以下、好ましくは9.0以下、より好ましくは8.5以下、さらに好ましくは8.0以下、よりさらに好ましくは7.5以下、よりさらに好ましくは7.0以下、よりさらに好ましくは6.5以下、よりさらに好ましくは6.0以下の条件で、40℃以上、好ましくは42℃以上、より好ましくは43℃以上、さらに好ましくは45℃以上、65℃以下、好ましくは62℃以下、より好ましくは60℃以下、さらに好ましくは57℃以下、よりさらに好ましくは55℃以下、よりさらに好ましくは52℃以下、よりさらに好ましくは50℃以下の温度で熱処理した後、高圧分散装置を用いて物理的処理をする、藻類の破砕方法。
前記微細藻類が、ナンノクロロプシス属である、前記<1>に記載の藻類の破砕方法。
前記熱処理は、好ましくは0.5時間以上、より好ましくは1時間以上、さらに好ましくは3時間以上、よりさらに好ましくは5時間以上、よりさらに好ましくは8時間以上、よりさらに好ましくは10時間以上、よりさらに好ましくは20時間以上、よりさらに好ましくは24時間以上、よりさらに好ましくは48時間以上である、前記<1>又は<2>に記載の藻類の破砕方法。
前記熱処理は、好ましくは96時間以下、より好ましくは72時間以下である、前記<1>~<3>のいずれか1つに記載の藻類の破砕方法。
前記物理処理は、前記高圧分散装置を用い、ゲージ圧で好ましくは10MPa以上、より好ましくは30MPa以上、さらに好ましくは50MPa以上、よりさらに好ましくは80MPa以上、好ましくは200MPa以下、より好ましくは150MPa以下、さらに好ましくは120MPa以下の圧力を加えた後、絶対圧で、好ましくは0.3MPa以下、より好ましくは0.2MPa以下、さらに好ましくは0.15MPa以下、よりさらに好ましくは0.11MPa以下、よりさらに好ましくは大気圧(0.1MPa)に減圧する、前記<1>~<4>のいずれか1つに記載の藻類の破砕方法。
前記熱処理は、細胞壁を分解する酵素の意図的な添加なしに行う、前記<1>~<5>のいずれか1つに記載の藻類の破砕方法。
前記熱処理は、pHが5.0以上、7.5以下の条件で、温度が45℃以上、60℃以下で、時間を10時間以上行う、前記<1>~<6>のいずれか1つに記載の藻類の破砕方法。
高圧分散装置が、均質バルブ式の高圧分散装置又はチャンバ式の高圧分散装置である、<1>~<7>のいずれか1つに記載の藻類の破砕方法。
<1>~<8>のいずれか1つに記載された藻類の破砕方法により得られた藻類の破砕物から脂質を回収する、藻類から脂質を抽出する方法。
前記脂質を回収する処理は、溶媒抽出、遠心分離、静置処理、及びカラムクロマトグラフィーから選ばれた1種又は2種以上の組み合わせであり、好ましくは溶媒抽出、遠心分離及び静置処理から選ばれる1種又は2種以上の組み合わせであり、より好ましくは溶媒抽出と遠心分離との組み合わせ、又は溶媒抽出と静置処理との組み合わせである、前記<9>に記載の藻類から脂質を抽出する方法。
前記脂質を回収する処理における、溶媒抽出に用いる溶媒が、好ましくは非極性溶媒であり、より好ましくは炭化水素類であり、さらに好ましくはヘキサンである、前記<10>に記載の藻類から脂質を抽出する方法。
前記脂質を回収する処理における、溶媒抽出の温度が、好ましくは10℃以上、より好ましくは20℃以上であり、好ましくは60℃以下、より好ましくは50℃以下、さらにより好ましくは40℃以下である、前記<10>又は<11>に記載の藻類から脂質を抽出する方法。
前記脂質を回収する処理における、遠心分離の遠心力が、好ましくは500G以上、より好ましくは1000G以上であり、好ましくは10000G以下、より好ましくは5000G以下、さらに好ましくは2000G以下である、前記<10>~<12>のいずれか1つに記載の藻類から脂質を抽出する方法。
前記脂質を回収する処理における、遠心分離の処理時間が、好ましくは1分以上、より好ましくは5分以上、さらに好ましくは10分以上であり、好ましくは80分以下、より好ましくは40分以下、さらに好ましくは20分以下である、前記<10>~<13>のいずれか1つに記載の藻類から脂質を抽出する方法。
前記脂質を回収する処理における、遠心分離の処理温度が、好ましくは10℃以上、より好ましくは15℃以上であり、好ましくは50℃以下、より好ましくは40℃以下である、前記<10>~<13>のいずれか1つに記載の藻類から脂質を抽出する方法。
沖縄県石垣島近郊の沿岸から藻体含む海水サンプルを取得した。取得した海水サンプルをフィルタによって濃縮し、マイクロピペットにより一つの藻体株を単離した。この単離した藻体は、培養液(ダイゴIMK培地、和光純薬工業社製)によって培養を行い、さらに培養液(f/2培地)を用いて藻体を増殖させた。この藻体の一部をテキサス大学(UTEX Culture Collection)に分析を依頼し、ナンノクロロプシス・サリナ(Nannochloropsis salina)であることが同定された。
希釈した処理液2μLをバクテリアカウンター(サンリード硝子製)の計算室に注入した後、光学顕微鏡(Nikon製、ECLIPSE80i)を用いて観察倍率400倍で観察し、ブロック内の細胞数をカウントした。バクテリアカウンターの計算室のうち、0.05mm角のブロックを使用した。計算室には、0.05mm角のブロック16マス(縦4マス×横4マス)からなる集合体が、25個(縦5個×横5個)並んでいる。これらの集合体のうち、顕微鏡の観察画面の右上から左下までの対角線上に存在する5個の集合体中に含まれる細胞数をカウントした。すなわち、0.05mm角のブロックの80マス(16マス×5個)中の細胞数をカウントした。バクテリアカウンターの計算室の深さは0.020mmであり、0.05mm角のブロック1つあたりの体積は1/20000mm3である。カウントした細胞の総数を、該当するブロックの体積(1/20000mm3×80マス)で除し、さらにカウントに用いた希釈液の希釈倍率をこれに乗ずることにより、希釈前のサンプル1mLあたりの細胞数を求めた。なお、希釈液には、ダイゴ人工海水SP(和光純薬工業製)を用いた。
前述の細胞数の測定方法により、処理液中の細胞数を測定した。破砕処理前の細胞数から破砕処理後の細胞数を引いて、破砕処理前の細胞数で除し、100を乗じた値を細胞破砕率(%)とした。
微細藻類を含む処理液を遠心分離機(HITACHI社製、CR22GIII、ローター:18A)にて、遠心分離(15000rpm、5分、25℃)し、上清を捨てた後、0.125Mクエン酸-リン酸水素二ナトリウムバッファー(pH5)に再分散させた。再分散させた液をフィルタ(日本ポール製、Supor-450、孔径0.45μm)にて吸引ろ過し、等量の蒸留水で掛け洗いした。藻体を捕集したフィルタをアルミカップに移して105℃で2時間乾燥させた。乾燥後の重量を測定し、フィルタの風袋を差し引いて藻体濃度(g/L)とした。また、処理液がフィルタで吸引ろ過しにくい場合は、適当な濃度に処理液を希釈して、乾燥後の重量を測定し、フィルタの風袋を差し引いた後、希釈率を乗じて藻体濃度(g/L)とした。なお、希釈液には、0.125Mクエン酸-リン酸水素二ナトリウムバッファー(pH5)を用いることができる。
所定濃度の微細藻類を含む処理液を、ポリエチレン製の容器に入れ、予め所定の温度に設定した真空乾燥機(ヤマト科学社製、ADP300)のチャンバ内に静置した。チャンバ内は大気圧とした。所定の時間が経過した後、サンプルを乾燥機から取り出し、室温にて冷却した。なお、比較として25℃で処理する場合は、実験室の温度を25℃とし、実験室内にサンプルを静置した。また、比較として4℃で処理する場合は、冷蔵庫(三洋電機株式会社製、MPR-1411)内にサンプルを静置した。所定の時間が経過した後、サンプルを冷蔵庫から取り出し、室温に戻した。
物理的処理は、高圧分散装置により行った。高圧分散装置には、ナノヴェイタ「NM2-L200-D」(吉田機械興業社製、クロス型ノズル:NVGL-XT160)又は圧力式ホモジナイザー「LAB2000」(株式会社エスエムテー社製)を用いた。ナノヴェイタを用いた場合は、処理圧力は、入口圧がゲージ圧で100MPa、出口圧が絶対圧で0.1Mpa(大気圧)とし、端切りのために7ショット目から取得した。パス回数は1回とした。圧力式ホモジナイザーを用いた場合は、処理圧力は、入口圧がゲージ圧で100MPa、出口圧が絶対圧で0.1Mpa(大気圧)とした。端切りのために処理開始後の300ccの処理液は廃棄し、300cc以降から処理サンプルとして取得した。パス回数は1回とした。
藻体の脂質の含量は、E.G.BlighとW.J.Dyerによって1959年に報告された生体材料からの脂質の抽出方法(Bligh & Dyer法)に従って分析した(E.G.Bligh、W.J.Dyer、Canadian journal of biochemistry and physiology、37(1959)、p.911-917)。
装置:Agilent technology 7890A
カラム:DB1-MS(J&W scientific製、20m×100μm×0.1μm)
オーブン温度:150℃(0.5min hold)-[40℃/min]-220℃(0min hold)-[20℃/min]-320℃(2min hold)-post run2min
キャリアガス:水素
メイクアップガス:ヘリウム
サンプル注入量:5μL
注入法:スプリットモード(スプリット比=75:1)
注入口温度:300℃
検出器:FID
カラム流量:0.28mL/minコンスタント
圧力(ゲージ圧):62.403psi
標準物質:SIGMA社製の下記脂肪酸エステルを用いた。
ラウリン酸メチル(C12)、ミリスチン酸メチル(C14)、パルミチン酸メチル(C16)、ステアリン酸メチル(C18)、パルミトレイン酸メチル(C16:1)、オレイン酸メチル(C18:1)、リノール酸メチル(C18:2)、リノレン酸メチル(C18:3)、エイコサペンタエン酸メチル(C20:5)、ドコサヘキサエン酸メチル(C22:6)
脂質は以下に示す溶媒抽出により回収した。回収した脂質は、メチルエステル化した後、前述のGCにて脂質量を定量した。
処理後の試料0.5mLに、ヘキサン1mLを添加し、25℃にて3分間撹拌した後、遠心分離機、「himacCF7D2」(日立工機株式会社製)を用いて遠心分離(遠心力:1500G、回転数:3000r/min、温度:25℃、時間:15分間)した。次に、上層のヘキサン相を400μL採取し、内部標準として1mg/mLの7-ペンタデカノン(メタノール溶液)を40μL添加した後、窒素を用いて乾固した。次に、0.7mLの0.5N KOH-メタノール溶液(水酸化カリウム2.8g、メタノール100mL)を添加し、80℃で30分間保温してケン化を行った。さらに1mLの14%三フッ化ホウ素溶液を添加し、80℃にて10分間保温してメチルエステル化を行い、溶媒と飽和食塩水をそれぞれ1mL添加して撹拌した後、25℃で30分間放置して溶媒相を取得した。溶媒にはヘキサンを用いた。得られた溶媒相を回収し、脂肪酸エステルの同定及び定量を前述の条件のGCにより行った。またGC分析にて検出した脂肪酸エステルの量を、内部標準を基準にして算出し、その総量をヘキサン中の脂質量として求めた。
以下の式(1)によりヘキサン溶媒による脂質回収率を算出した。
脂質回収率(%)=ヘキサン中の脂質量/乾燥藻体中の脂質量×100・・・(1)
不等毛植物門に属する微細藻類としてナンノクロロプシス・サリナ(Nannochloropsis salina)(処理液を構成する液体:人工海水(ダイゴ人工海水SP、日本製薬株式会社製、藻体濃度:1.0g/L))を用いた。25℃における処理液のpHは7.3であった。1MのHClを滴下し、処理液のpHを5.0に調整した。pHを調整した溶液に対して熱処理を行った。処理温度は50℃とし、処理時間は1時間とした。熱処理後に、物理的処理をナノヴェイタを用いて入口圧が100MPaの条件で行った。細胞の破砕率は38.6%であった。
熱処理時間を2時間とした以外は実施例1と同様にした。細胞の破砕率は33.9%であった。
熱処理時間を3時間とした以外は実施例1と同様にした。細胞の破砕率は45.8%であった。
熱処理時間を5時間とした以外は実施例1と同様にした。細胞の破砕率は47.4%であった。
熱処理時間を10時間とした以外は実施例1と同様にした。細胞の破砕率は60.5%であった。
熱処理時間を24時間とした以外は実施例1と同様にした。細胞の破砕率は87.0%であった。また、破砕後の脂質回収率は69%であった。
物理的処理における入口圧力を50MPaとした以外は実施例6と同様にした。細胞の破砕率は75.9%であった。また、破砕後の脂質回収率は70%であった。
pHの調整をせず、熱処理も行わなかったこと以外は、実施例1と同様にした。すなわちナンノクロロプシス・サリナ(Nannochloropsis salina)(処理液を構成する液体:人工海水(ダイゴ人工海水SP、日本製薬株式会社製、藻体濃度:1.0g/L))の処理液を得た後、pH7.3のまま、サンプル取得後30分以内に熱処理を行わずに高圧分散装置ナノヴェイタにて物理的処理を入口圧100MPaの条件で行った。細胞の破砕率は16.9%であった。
熱処理を行わなかったこと以外は、実施例1と同様にした。すなわちナンノクロロプシス・サリナ(Nannochloropsis salina)(処理液を構成する液体:人工海水(ダイゴ人工海水SP、日本製薬株式会社製、藻体濃度:1.0g/L))の処理液を、1MのHClを用いて25℃にてpH5.0に調整した後、30分以内に熱処理を行わずに高圧分散装置ナノヴェイタにて物理的処理を入口圧100MPaの条件で行った。細胞の破砕率は18.7%であった。また、破砕後の脂質回収率は6%であった。
熱処理温度を25℃とした以外は、実施例1と同様にした。細胞の破砕率は16.1%であった。
熱処理温度を25℃とし、熱処理時間を2時間とした以外は、実施例1と同様にした。細胞の破砕率は11.9%であった。
熱処理温度を25℃とし、熱処理時間を3時間とした以外は、実施例1と同様にした。細胞の破砕率は13.2%であった。
熱処理温度を25℃とし、熱処理時間を10時間とした以外は、実施例1と同様にした。細胞の破砕率は18.5%であった。
熱処理温度を25℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は16.1%であった。
熱処理温度を80℃とした以外は、実施例1と同様にした。細胞の破砕率は21.8%であった。
熱処理温度を80℃とし、熱処理時間を2時間とした以外は、実施例1と同様にした。細胞の破砕率は18.5%であった。
熱処理温度を80℃とし、熱処理時間を3時間とした以外は、実施例1と同様にした。細胞の破砕率は24.8%であった。
熱処理温度を80℃とし、熱処理時間を10時間とした以外は、実施例1と同様にした。細胞の破砕率は18.5%であった。
熱処理温度を80℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は23.0%であった。
比較例2と同様にして破砕処理を行った後、50℃で、24時間の熱処理を行った。細胞の破砕率は19.3%であった。
熱処理温度を40℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は49.5%であった。また、破砕後の脂質回収率は33%であった。
熱処理温度を45℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は92.0%であった。また、破砕後の脂質回収率は74%であった。
熱処理温度を55℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は81.2%であった。また、破砕後の脂質回収率は73%であった。
熱処理温度を60℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は72.1%であった。また、破砕後の脂質回収率は55%であった。
熱処理温度を4℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は19.9%であった。
熱処理温度を37℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は19.0%であった。
熱処理温度を70℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は29.4%であった。
熱処理温度を80℃とし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は23.0%であった。
1MのHClを用いて処理液のpHを25℃にて4.0に調整し、熱処理時間を10時間とした以外は、実施例1と同様にした。細胞の破砕率は40.3%であった。
熱処理時間を24時間とした以外は、実施例12と同様にした。細胞の破砕率は66.0%であった。
処理液のpHを25℃にて6.8に調整し、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は53.5%であった。
処理液のpHの調整をせず、25℃におけるpHを7.3のままとし、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は52.3%であった。
熱処理時間を48時間とした以外は、実施例15と同様にした。細胞の破砕率は66.6%であった。
1MのNaOHを用いて処理液のpHを25℃にて9.0に調整し、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は47.4%であった。
1MのHClで処理液のpHを25℃にて2.0に調整し、熱処理時間を24時間とした以外は、実施例1と同様にした。細胞の破砕率は23.6%であった。
1MのHClで処理液のpHを25℃にて3.0に調整し、熱処理時間24時間とした以外は、実施例1と同様にした。細胞の破砕率は16.0%であった。
1MのNaOHで処理液のpHを25℃にて10.0に調整し、熱処理時間24時間とした以外は、実施例1と同様にした。細胞の破砕率は26.5%であった。
1MのNaOHで処理液のpHを25℃にて12.0に調整し、熱処理時間24時間とした以外は、実施例1と同様にした。細胞の破砕率は18.6%であった。
不等毛植物門に属する微細藻類としてナンノクロロプシス・オキュラータ(Nannochloropsis oculata)「冷蔵ナンノ ヤンマリンK-1」(クロレラ工業製、処理液を構成する液体:海水、藻体濃度:50g/L)を室温に戻して用いた。さらにこの処理液を人工海水(日本製薬株式会社製、海産微細藻類用ダイゴ人工海水SP)で希釈し、藻体濃度を1.0g/Lとした。処理液の25℃におけるpHは5.0であった。以上の処理液を用いて、熱処理時間を5時間とした以外は、実施例1と同様にした。細胞の破砕率は47.4%であった。
熱処理時間を10時間とした以外は、実施例18と同様にした。細胞の破砕率は49.4%であった。
pHの調整をせず、熱処理を行わなかったこと以外は、実施例18と同様にした。すなわちナンノクロロプシス・オキュラータ「冷蔵ナンノ ヤンマリンK-1」(藻体濃度:1.0g/L)の処理液を、25℃におけるpHを6.8としたまま、希釈後30分以内に熱処理を行わずに高圧分散装置にて物理的処理を行った。細胞の破砕率は19.6%であった。
熱処理温度を25℃とし、熱処理時間を10時間とした以外は、実施例18と同様にした。細胞の破砕率は22.7%であった。
不等毛植物門に属する微細藻類としてナンノクロロプシス・サリナ(Nannochloropsis salina)(処理液を構成する液体:人工海水(ダイゴ人工海水SP、日本製薬株式会社製、藻体濃度:1.0g/L))を用いた。処理液のpHは7.3であった。この処理液に1MのHClを滴下し、処理液のpHを25℃にて6.3に調整した後、硫酸アルミニウム(セントラル硝子株式会社社製、商品名「硫酸バンド」)を処理液に対し0.1%となるように添加して5分間撹拌した。その後、撹拌を停止し、室温で3時間静置した。この時藻体が凝集し、沈降した。その後、上清の一部を廃棄して藻体濃度を15.2g/Lとした。1MのHClを滴下し、処理液のpHを25℃にて5.0に調整した。pHを調整した溶液に対して熱処理を行った。処理温度は50℃とし、処理時間は24時間とした。熱処理後に、物理的処理を圧力式ホモジナイザーを用いて入口圧が100MPaの条件で行った。細胞の破砕率は77.6%であった。
101 均質バルブシート
102 均質バルブ本体
103 インパクトリング
110 チャンバ
111 流入管路
112 せん断管路
113 流出管路
120 チャンバ
121 流入管路
122 せん断管路
123 流出管路
Claims (9)
- 不等毛植物門に属する微細藻類に対し、pHが3.5以上、9.5以下の条件で40℃以上、65℃以下の温度で熱処理した後、高圧分散装置を用いて物理的処理をする、藻類の破砕方法。
- 前記微細藻類が、ナンノクロロプシス属である、請求項1に記載の藻類の破砕方法。
- 前記熱処理は、前記pHが、5.0以上、7.5以下の条件で行う、請求項1又は2に記載の藻類の破砕方法。
- 前記熱処理は3時間以上行う、請求項1~3のいずれか1項に記載の藻類の破砕方法。
- 前記熱処理は10時間以上行う、請求項1~3のいずれか1項に記載の藻類の破砕方法。
- 前記熱処理は45℃以上、60℃以下の温度で行う、請求項1~5のいずれか1項に記載の藻類の破砕方法。
- 前記熱処理は、pHが5.0以上、7.5以下の条件で、温度が45℃以上、60℃以下で、時間を10時間以上行う、請求項1又は2に記載の藻類の破砕方法。
- 前記高圧分散装置が、均質バルブ式の高圧分散装置又はチャンバ式の高圧分散装置である、請求項1~6のいずれか1つに記載の藻類の破砕方法。
- 請求項1~8のいずれか1項に記載された藻類の破砕方法により得られた藻類の破砕物から脂質を回収する、藻類から脂質を抽出する方法。
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