WO2008072381A1 - 固定化酵素を用いた有用物質の製造方法 - Google Patents
固定化酵素を用いた有用物質の製造方法 Download PDFInfo
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- WO2008072381A1 WO2008072381A1 PCT/JP2007/001401 JP2007001401W WO2008072381A1 WO 2008072381 A1 WO2008072381 A1 WO 2008072381A1 JP 2007001401 W JP2007001401 W JP 2007001401W WO 2008072381 A1 WO2008072381 A1 WO 2008072381A1
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- packed
- enzyme
- reaction
- immobilized enzyme
- useful substance
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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
- C12P7/40—Preparation of oxygen-containing organic compounds containing a carboxyl group including Peroxycarboxylic acids
-
- 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
- C12N11/00—Carrier-bound or immobilised enzymes; Carrier-bound or immobilised microbial cells; Preparation thereof
-
- 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
- C12N9/00—Enzymes; Proenzymes; Compositions thereof; Processes for preparing, activating, inhibiting, separating or purifying enzymes
- C12N9/14—Hydrolases (3)
- C12N9/16—Hydrolases (3) acting on ester bonds (3.1)
- C12N9/18—Carboxylic ester hydrolases (3.1.1)
- C12N9/20—Triglyceride splitting, e.g. by means of lipase
-
- 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
- C12P7/62—Carboxylic acid esters
-
- 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
Definitions
- the present invention relates to a method for producing a useful substance by a reaction using a fixed bed type reaction column packed with an immobilized enzyme.
- Immobilized enzymes used for L-aspartic acid production, transesterified oil and fat production, lactose hydrolysis, fat and oil hydrolysis, etc. are conducted by passing a liquid through a fixed bed type reaction tower.
- the reaction used is known. Since these reactions all have a relatively small calorific value, the simplest drum reactor is usually used.
- reaction liquids are uniformly mixed from the viewpoint of improving reaction efficiency.
- the liquid is preferably passed in the state.
- the oil phase substrate and the aqueous phase substrate used for the hydrolysis do not usually become one phase even when mixed, so it is common to use emulsion.
- emulsion particles are difficult to reach the enzyme adsorbed in the pores of the carrier, there is a technique in which the liquid flow rate is within a range where the reaction solution is not emulsified (see Patent Document 1).
- Patent Documents 1 and 2 As a method of circulating an oil phase substrate and an aqueous phase substrate through a fixed bed, a method of flowing in a countercurrent (see Patent Documents 1 and 2) and a method of circulating in a parallel flow (Patent Document 3).
- Patent Documents 1 and 2 As a method of circulating an oil phase substrate and an aqueous phase substrate through a fixed bed, a method of flowing in a countercurrent (see Patent Documents 1 and 2) and a method of circulating in a parallel flow (Patent Document 3).
- Patent Document 3 since the former requires a special mechanism and operation method, it is generally adopted to distribute in parallel flow.
- Patent Document 1 JP-A-6 1-8 5 1 95
- Patent Document 2 Japanese Patent Laid-Open No. 1-9 8 4 94
- Patent Document 3 Japanese Patent Laid-Open No. 2 00 0 _ 1 6 0 1 8 8
- the present invention relates to a liquid that forms a two-liquid phase in a fixed bed type reaction tower packed with an immobilized enzyme.
- a method for producing a useful substance in which a mixture is fed and reacted in the same direction in the same direction the packed thickness of the immobilized enzyme per stage of a fixed bed reactor having an equivalent circle diameter of 35 mm 0 or more
- the present invention provides a method for producing a useful substance having a value of 10 to 20 O mm.
- the present invention also provides a method for producing a useful substance in which a liquid mixture that forms a two-liquid phase is supplied to a fixed bed type reaction column packed with an immobilized enzyme, and the reaction is caused to flow in the same direction.
- a packed part filled with an immobilized enzyme having a packed thickness of 10 to 20 O mm per stage of a fixed bed type reaction tower having an equivalent diameter of 35 mm 0 or more is an empty space having a thickness equal to or less than the packed thickness.
- the present invention provides a method for producing a useful substance using a multistage fixed bed type reaction tower in which at least two stages are stacked with a part interposed therebetween.
- the present invention also provides a fixed bed type reaction tower having an equivalent circle diameter of 35 mm 0 or more and a packed thickness of immobilized enzyme per stage of 10 to 20 O mm.
- the present invention provides a method for producing a useful substance in which a reaction is performed by circulating a liquid mixture forming a two-liquid phase through a fixed bed type reaction tower packed with an immobilized enzyme.
- the present invention relates to a method for producing a useful substance more efficiently by increasing reactivity and improving productivity.
- the present invention in a method for producing a useful substance by supplying a liquid mixture that forms a two-liquid phase to a fixed bed type reaction column packed with an immobilized enzyme, the entire reaction liquid in the column is obtained.
- the flow can be made uniform, and as a result, the reactivity and productivity can be improved.
- the enzyme activity is effectively expressed, and fatty acids can be produced efficiently.
- a liquid mixture (reaction solution) that forms a two-liquid phase is supplied to a fixed bed type reaction tower packed with an immobilized enzyme.
- a fixed bed type reaction tower hereinafter also referred to as “enzyme tower” means that the immobilized enzyme is packed in a column or the like so that the reaction solution can be circulated through the space between the immobilized carriers and the pores of the immobilized carrier. This is what you made.
- the fixed bed type reaction tower may be composed of a single fixed bed type reactor having a single packed portion packed with an immobilized enzyme, and the packed portion is sandwiched between two empty stages.
- a multi-stage fixed bed type reaction tower laminated as described above may be used.
- the two-liquid phase means a state in which two types of liquids do not become one phase even after mixing, and includes those in which they are phase-separated or even in an emulsified state.
- an enzyme in which an oleolytic enzyme is adsorbed on an immobilization carrier is used as an immobilization enzyme, and an oil phase substrate and an aqueous phase substrate are used as two liquid phases in an enzyme tower packed with the enzyme. It is preferable that the fatty acid is produced as a useful substance by hydrolysis reaction of fats and oils by circulating the oil.
- the two liquid phases are made to flow in the same direction.
- the two liquid phases may be mixed in advance and supplied as an emulsified state, or may be supplied while being separated. Further, the two liquid phases may be alternately supplied at regular intervals.
- Each substrate may be supplied to the enzyme tower in a downward flow from the tower top to the tower bottom or in an upward flow from the tower bottom to the tower top.
- the immobilized enzyme used in the present invention is one in which an enzyme is supported on an immobilized carrier by adsorption or the like.
- the immobilization carrier celite, diatomaceous earth, force orientate , Silica gel, molecular sieve, porous glass, activated carbon, calcium carbonate, ceramics and other inorganic carriers, ceramic powder, polyvinyl alcohol, polypropylene, chitosan, ion exchange resin, hydrophobic adsorption resin, chelate resin, synthesis
- An organic polymer such as an adsorbent resin can be mentioned, and an ion exchange resin is particularly preferable because of its high water retention capability.
- a porous surface is preferable because it has a large surface area and can increase the amount of adsorbed enzyme.
- the particle diameter of the resin used as the immobilization carrier is preferably 100 to 1 O 2 O m, more preferably 250 to 750 m.
- the pore diameter is preferably from 10 to 150 nm, and more preferably from 10 to 100 nm.
- the material include phenol formaldehyde, polystyrene, acrylamide, divinylbenzene, and the like, particularly phenol formaldehyde resin (for example Duolite A-568 manufactured by Rohm and Hass). This is preferable from the viewpoint of improving the enzyme adsorption.
- the enzyme used for the immobilized enzyme of the present invention is not particularly limited, but lipase as an enzyme for decomposing oils and fats is preferable from the viewpoint of a large productivity improvement effect.
- lipase not only those derived from animals and plants but also commercially available lipases derived from microorganisms can be used.
- Microbial lipases include: Rhizopus 1 i, Aspergi II us Mucor, Pseud omo nas I ⁇ , Geotrich um; I ⁇ , Penici II ium genus, Candida genus and so on.
- the temperature at which the enzyme is immobilized can be determined depending on the properties of the enzyme, but it is preferably 0 to 60 ° C, particularly 5 to 40 ° C, where the enzyme is not deactivated.
- the pH of the enzyme solution used for immobilization may be in a range where no denaturation of the enzyme occurs and can be determined by the enzyme characteristics as well as the temperature, but pH 3-9 is preferred.
- a buffer solution is used. Examples of the buffer solution include an acetate buffer solution, a phosphate buffer solution, and a tris hydrochloride buffer solution.
- Enzyme dissolution The enzyme concentration in the solution is preferably not more than the saturation solubility of the enzyme from the viewpoint of immobilization efficiency, and a sufficient concentration.
- the enzyme solution a supernatant obtained by removing an insoluble part by centrifugation, if necessary, or a solution purified by ultrafiltration can be used.
- the enzyme mass to be used varies depending on the enzyme activity, but is preferably 5 to 100 mass%, particularly preferably 10 to 500 mass%, based on the mass of the carrier.
- the carrier and the enzyme may be directly adsorbed.
- the carrier in order to obtain an adsorption state that exhibits high activity, the carrier is preliminarily fixed with a fat-soluble fatty acid or a derivative thereof before the enzyme adsorption. It is preferable to treat with.
- these may be added directly to water or an organic solvent.
- the fat-soluble fatty acid or derivative thereof is once dispersed in the organic solvent. After dissolution, it may be added to a carrier dispersed in water.
- the organic solvent include black mouth form, hexane, ethanol and the like.
- the mass of the fat-soluble fatty acid or derivative thereof used is preferably 1 to 500 mass%, particularly preferably 10 to 200 mass%, based on the mass of the carrier.
- the contact temperature is preferably 0 to 100 ° C., particularly preferably 20 to 60 ° C., and the contact time is preferably about 5 minutes to 5 hours.
- the carrier after this treatment is recovered by filtration, but may be dried.
- the drying temperature is preferably room temperature to 100 ° C., and may be dried under reduced pressure.
- the fat-soluble fatty acid is a saturated or unsaturated, linear or straight chain having 4 to 24 carbon atoms, preferably 8 to 18 carbon atoms.
- examples include branched-chain fatty acids which may have a hydroxyl group. Specific examples include strong puric acid, lauric acid, myristic acid, oleic acid, linoleic acid, monolinolenic acid, ricinoleic acid, and isostearic acid.
- the fat-soluble fatty acid derivatives include esters of these fat-soluble fatty acids with monohydric or polyhydric alcohols or saccharides, phospholipids, and those obtained by adding ethylene oxide to these esters. Specific examples include methyl esters, ethyl esters, monoglycerides, diglycerides, ethylene oxide adducts thereof, polyglycerin esters, sorbitan esters, and sucrose esters of the above fatty acids. These fat-soluble fatty acids and their derivatives It is preferable in the process of immobilizing the enzyme on the carrier that all conductors are liquid at room temperature. As these fat-soluble fatty acids or derivatives thereof, two or more of the above may be used in combination, and naturally derived fatty acids such as rapeseed fatty acid and soybean fatty acid may be used.
- the hydrolytic activity of the immobilized enzyme is preferably 20 U / g or more, more preferably 10 00 to 1 O O O O U Z g, and particularly preferably in the range of 5 00 to 5 00 0 U / g.
- the hydrolysis activity (U / g—o i I) of the immobilized enzyme given per unit mass of fats and oils and the time required to reach a certain hydrolysis rate are in an inversely proportional relationship.
- the volume of the immobilized enzyme packed part is multiplied by the porosity of the packed part, the volume ratio of the fats and oils in the reaction solution, and the specific gravity of the fats and oils. Ask.
- the oil phase substrate mainly refers to vegetable oils, animal oils, or oils and combinations thereof, but the oils and fats may contain diacyl glycerol, monoacyl glycerol, or fatty acids in addition to triacylglycerol. It may contain fatty acids obtained as a result of hydrolysis.
- Specific examples of the oil phase substrate include vegetable oils such as rapeseed oil, soybean oil, castor oil, palm oil and flax oil, animal oils such as beef tallow, pork tallow and fish oil, etc., or a combination of these oils and fats. .
- These fats and oils can use deodorized oil and non-deodorized fats and oils that have not been deodorized in advance. However, non-deodorized fats and oils are used for some or all of these fats and oils. It is preferable from the viewpoint that trans unsaturated fatty acids and conjugated unsaturated fatty acids can be reduced and plant sterols, plant sterol fatty acid esters and tocopherols derived from raw oils and fats can be left. In the oil phase substrate, oil-soluble components such as fatty acids may be mixed in addition to the fats and oils.
- Fatty acids refer to fatty acids obtained as a result of hydrolysis, as well as those containing one or more of the above glycerides.
- the other one of the liquid mixtures forming the two liquid phases used in the present invention is preferably an aqueous phase matrix.
- the aqueous phase substrate is water, but other water-soluble components such as glycerin obtained as a result of hydrolysis may be mixed.
- the reaction is carried out using an enzyme column having an equivalent circle diameter of 35 mm0 or more and a packed thickness of immobilized enzyme per stage of 10 to 20 Omm.
- the equivalent circle diameter of the enzyme tower becomes larger than 35 mm 0, the flow of the reaction liquid becomes uneven and the reactivity tends to decrease.
- the equivalent circle diameter of the enzyme column is preferably 35 to 10,000 mm 0, particularly 35 to 7, 50 Omm0, more preferably 35 to 5, O 2 O Omm0 in terms of reactivity and productivity.
- the equivalent circle diameter means the diameter of the enzyme tower when it is circular, and when it is a polygon, it means the diameter of a circle having the same area as the projected area, where the projected area is A and the following equation (1) Is required.
- the shape of the enzyme column used in the present invention may be any shape that can withstand the indentation pressure of the pump used. Moreover, it is preferable that a jacket is provided around the enzyme tower so that the reaction liquid flowing in the enzyme tower can be adjusted to a temperature suitable for the enzyme reaction.
- the temperature in the enzyme tower is preferably 0 to 60 ° C, more preferably 20 to 40 ° C, in order to extract the activity of the immobilized enzyme more effectively.
- the length of the enzyme column may be as long as necessary to obtain the desired decomposition rate, but from the standpoints of reactivity, pressure loss in the column, etc., 0.1-1 Om, preferably 0.1-5m Preferably in the range Yes.
- the immobilized enzyme is packed in the enzyme column so that the packing thickness per stage is 10 to 200 mm.
- the packed thickness of the immobilized enzyme per stage in the enzyme tower is preferably a force of 10 to 20 Omm, more preferably 15 to 200 mm, especially 75 to 20 Omm from the viewpoint of reactivity.
- the empty space provided between the packed sections filled with the immobilized enzyme is less than the packed thickness of the immobilized enzyme in terms of reactivity, production, etc.
- the thickness is preferably 1 to 200 mm, particularly 5 to 200 mm, and more preferably 15 to 20 Omm.
- the filling part is preferably laminated in 2 to 30 stages, particularly 3 to 20 stages with the empty part in between, from the viewpoint of reactivity, production and the like.
- reaction liquid to the enzyme tower it may be carried out separately by piping directly connected to the enzyme tower, or may be supplied by a common pipe. From the above, it is preferable to carry out piping separately connected to the enzyme tower.
- the flow rate of the reaction liquid in the enzyme column is preferably 1 to 40 Omm / min, more preferably 5 to 20 Omm / min.
- the liquid passing linear velocity (mm / min), feed volume per minute (mm 3 / min) (or feed rate (1 0_ 3 m L / min) also referred to as) the filling layer cross-sectional area of (mm 2 The value expressed by the quotient divided by).
- the liquid passage speed is 40 Omm / min or less.
- the flow rate is 1 mm / min or more. Since the expression activity of the immobilized enzyme changes depending on the flow rate, the optimal flow rate can be selected to determine the reaction conditions. Can respond to production capacity and manufacturing costs.
- the residence time of the reaction solution in the immobilized enzyme packing section in the enzyme tower is from the viewpoint of avoiding the equilibrium state of the hydrolysis reaction, more effectively extracting the activity of the immobilized enzyme, and improving productivity. Second to 60 minutes, more preferably 1 to 40 minutes.
- the residence time (minutes) is expressed as a value obtained by multiplying the thickness (mm) of the packed bed by the porosity and dividing this by the liquid linear velocity (mm / minute).
- the reaction solution that has passed through the enzyme tower may be used as a reaction-finished product as it is in view of reactivity, productivity, and the like, and the reaction solution is once separated into oil and water to separate the oil phase. Later, fresh water may be added and supplied again to the same enzyme tower in the same manner as described above, and may be passed repeatedly until the desired reaction rate is obtained.
- the reaction solution may be once separated into oil and water, and after separating the oil phase, fresh water may be added and supplied to another enzyme tower again by the same method as described above to carry out a continuous reaction.
- the oil phase is supplied to the next enzyme tower and the aqueous phase is supplied to the previous enzyme tower.
- an oil-water separation method of the reaction liquid an oil-water separator such as a natural sedimentation type or a centrifugal separation type is generally used, but is not particularly limited.
- Duolite A-568 (Rohm and Hass, particle size distribution 100- "! 000 m) 1 part by mass was stirred for 1 hour in 10 parts by mass of N / 10 NaOH solution. After washing with 10 parts by mass of ion-exchanged water, 50 OmM phosphate buffer (pH 7) was equilibrated with 10 parts by mass, and then 50 mM phosphate buffer (pH 7) pH was equilibrated twice for 2 hours at 10 parts by mass, followed by filtration to recover the carrier, and ethanol substitution with 5 parts by mass of ethanol for 30 minutes.
- the immobilized enzyme was recovered and washed with 10 parts by mass of 5 OmM phosphate buffer (pH 7) to remove unimmobilized enzyme and protein. After that, 4 parts by mass of rapeseed oil to be actually decomposed was added and stirred for 12 hours. All the above operations were performed at 20 ° C. Then, it was filtered and separated from fats and oils to obtain an immobilized enzyme. As a result, an immobilized lipase having a hydrolysis activity (activity to be expressed) of 2700 U / g (dry mass) was obtained. The average particle size based on the mass of the immobilized enzyme was 3 1 1;
- a stainless steel column with a jacket (inner diameter 1 Omm, height 1400 mm) is packed with 27.0 g (dry mass) of the immobilized lipase (packing height 1 20 Omm), and the jacket is heated to 35 ° C. Keep warm. From the top of the column, a mixture of rapeseed oil and distilled water at a mass ratio of 10: 6 was fed at a rate of 1.57 mL / min, and the hydrolysis reaction was carried out. The results are shown in Table 1.
- a stainless steel column with a jacket (inner diameter 1 Omm, height 1 950 mm) was filled with 4.83 g of the above immobilized lipase on a dry basis (packing height 200 mm), and an empty space (height 1 50 mm).
- the hydrolysis reaction was carried out in the same procedure as in Reference Example 1 except that 6 layers were stacked with mm) in between. The results are shown in Table 1.
- the saponification value is Am e r i c a n
- a stainless steel column with a jacket was the same as in Example 1 except that 0.17825 kg of the immobilized lipase was packed on a dry basis (packing height 150 mm).
- the hydrolysis reaction was performed according to the procedure. Next, the reaction liquid that passed through the column was once separated into oil and water, and the oil phase was separated. Then, new water was added and mixed, and the mixture was supplied again to another column of the same shape. Went. The results are shown in Table 1.
- a stainless steel column with a jacket (inner diameter: 76.4 mm, height: 250 mm) is packed with 0.2 1 kg of the above immobilized lipase on a dry basis (packing height: 17 mm), and the feed rate is 92 mL.
- the hydrolysis reaction was performed in the same manner as in Example 1 except that the time was changed to / min. Next, the reaction solution that passed through the column was once separated into oil and water, and the oil phase was separated. Then, fresh water was added and mixed, and then supplied again to another power ram of the same shape. Reaction was performed. The results are shown in Table 1.
- a packed bed (packed height: 1 50 mm) filled with 13.37 kg of the above immobilized lipase on a dry base in a jacketed stainless steel column (inner diameter: 600 mm, height: 2250 mm)
- the hydrolysis reaction was carried out in the same procedure as in Example 1 except that the stacking was performed in 8 steps with a thickness of 1 50 mm in between, and the feeding speed was 5655 mL / min.
- Table 2 The results are shown in Table 2.
- Example 3 The procedure was the same as in Example 1, except that a jacketed stainless steel column (inner diameter: 70 mm, height: 3 O Omm) was filled with 0.35 kg of the immobilized lipase on a dry basis (packing height: 300 mm). Hydrolysis reaction was performed. Next, the reaction liquid that passed through the column was once separated into oil and water, and the oil phase was separated. Then, fresh water was added and mixed, and again supplied to another power ram of the same shape. Reaction was performed. The results are shown in Table 3.
- Example 1 except that a stainless steel column with a jacket (inner diameter 7 Omm, height 1 300 mm) was packed with 1.2 kg of the immobilized lipase on a dry basis (packing height 1 1 7 7 mm).
- the hydrolysis reaction was performed according to the procedure. The results are shown in Table 3.
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Abstract
Description
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Priority Applications (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CN2007800462899A CN101558160B (zh) | 2006-12-15 | 2007-12-14 | 使用固定化酶的有用物质的制造方法 |
US12/517,574 US8173403B2 (en) | 2006-12-15 | 2007-12-14 | Process for producing useful substance using immobilized enzyme |
EP07849831A EP2090661A4 (en) | 2006-12-15 | 2007-12-14 | METHOD FOR PRODUCING A USEFUL SUBSTANCE USING AN IMMOBILIZED ENZYME |
Applications Claiming Priority (2)
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JP2006-337890 | 2006-12-15 | ||
JP2006337890A JP4915732B2 (ja) | 2006-12-15 | 2006-12-15 | 固定化酵素を用いた有用物質の製造方法 |
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WO2008072381A1 true WO2008072381A1 (ja) | 2008-06-19 |
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US (1) | US8173403B2 (ja) |
EP (1) | EP2090661A4 (ja) |
JP (1) | JP4915732B2 (ja) |
KR (1) | KR20090097869A (ja) |
CN (1) | CN101558160B (ja) |
WO (1) | WO2008072381A1 (ja) |
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JP5242236B2 (ja) * | 2008-05-08 | 2013-07-24 | 花王株式会社 | 脂肪酸類の製造方法 |
WO2013114178A1 (en) * | 2012-01-30 | 2013-08-08 | Arvind Mallinath Lali | Enzymatic process for fat and oil hydrolysis |
Citations (4)
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JPS6185195A (ja) | 1984-10-02 | 1986-04-30 | Agency Of Ind Science & Technol | 脂質の連続加水分解法 |
JPH0198494A (ja) | 1987-10-09 | 1989-04-17 | Agency Of Ind Science & Technol | バイオリアクター |
JP2000160188A (ja) | 1998-11-26 | 2000-06-13 | Kao Corp | 油脂の加水分解方法 |
JP2000297295A (ja) * | 1999-04-14 | 2000-10-24 | Kao Corp | 油脂の加水分解方法 |
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US5292649A (en) * | 1983-03-29 | 1994-03-08 | Agency Of Industrial Science & Technology, Ministy Of International Trade & Industry | Method for reaction of lipase upon fatty acid |
US4629742A (en) * | 1986-01-27 | 1986-12-16 | Akzo America Inc. | Hydrolysis of fats |
DE19823332C2 (de) * | 1998-05-26 | 2000-09-07 | Unifar Kimya Sanayii Ve Ticare | Verfahren zur enzymatischen Herstellung von Betalactam-Antibiotika |
US6258575B1 (en) * | 1998-11-26 | 2001-07-10 | Kao Corporation | Hydrolyzing fats and oils using an immobilized enzyme column and substrate-feeding chamber that separates phases |
JP3764855B2 (ja) * | 2001-06-22 | 2006-04-12 | 花王株式会社 | 油脂類の加水分解方法 |
US8241875B2 (en) | 2005-06-21 | 2012-08-14 | Kao Corporation | Method for producing fatty acids with an immobilized enzyme packed column |
KR101294474B1 (ko) * | 2005-10-05 | 2013-08-07 | 카오카부시키가이샤 | 고정화 효소를 이용한 유용 물질의 제조 방법 |
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2006
- 2006-12-15 JP JP2006337890A patent/JP4915732B2/ja not_active Expired - Fee Related
-
2007
- 2007-12-14 WO PCT/JP2007/001401 patent/WO2008072381A1/ja active Application Filing
- 2007-12-14 EP EP07849831A patent/EP2090661A4/en not_active Withdrawn
- 2007-12-14 US US12/517,574 patent/US8173403B2/en not_active Expired - Fee Related
- 2007-12-14 KR KR1020097012038A patent/KR20090097869A/ko not_active Application Discontinuation
- 2007-12-14 CN CN2007800462899A patent/CN101558160B/zh not_active Expired - Fee Related
Patent Citations (4)
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JPS6185195A (ja) | 1984-10-02 | 1986-04-30 | Agency Of Ind Science & Technol | 脂質の連続加水分解法 |
JPH0198494A (ja) | 1987-10-09 | 1989-04-17 | Agency Of Ind Science & Technol | バイオリアクター |
JP2000160188A (ja) | 1998-11-26 | 2000-06-13 | Kao Corp | 油脂の加水分解方法 |
JP2000297295A (ja) * | 1999-04-14 | 2000-10-24 | Kao Corp | 油脂の加水分解方法 |
Non-Patent Citations (3)
Title |
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H-KITTIKUN A. ET AL.: "Continuous Production of Fatty Acids from Palm Olein by Immobilized Lipase in a Two-Phase System", J. AM. OIL. CHEM. SOC., vol. 77, no. 6, 2000, pages 599 - 603, XP008109277 * |
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WISDOM R.A. ET AL.: "Enzymatic Interesterification of Fats: Laboratory and Pilot-Scale Studies with Immobilized Lipase from Rhizopus arrhizus", BIOTECHNOL. BIOENG., vol. 29, no. 9, 1987, pages 1081 - 1085, XP009109242 * |
Also Published As
Publication number | Publication date |
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US8173403B2 (en) | 2012-05-08 |
CN101558160A (zh) | 2009-10-14 |
JP2008148596A (ja) | 2008-07-03 |
KR20090097869A (ko) | 2009-09-16 |
US20100047883A1 (en) | 2010-02-25 |
EP2090661A1 (en) | 2009-08-19 |
CN101558160B (zh) | 2012-07-18 |
EP2090661A4 (en) | 2012-04-04 |
JP4915732B2 (ja) | 2012-04-11 |
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