WO2020100598A1 - Procédé de production d'une dispersion aqueuse de polyhydroxyalcanoate - Google Patents

Procédé de production d'une dispersion aqueuse de polyhydroxyalcanoate Download PDF

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Publication number
WO2020100598A1
WO2020100598A1 PCT/JP2019/042634 JP2019042634W WO2020100598A1 WO 2020100598 A1 WO2020100598 A1 WO 2020100598A1 JP 2019042634 W JP2019042634 W JP 2019042634W WO 2020100598 A1 WO2020100598 A1 WO 2020100598A1
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pha
aqueous dispersion
polyhydroxyalkanoate
producing
weight
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English (en)
Japanese (ja)
Inventor
省二郎 大隅
彰仁 熊見
崇吉 長谷川
隼人 前田
郁弥 迫
智哉 西中
松村　邦彦
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Kaneka Corp
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Kaneka Corp
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D71/00—Semi-permeable membranes for separation processes or apparatus characterised by the material; Manufacturing processes specially adapted therefor
    • B01D71/06—Organic material
    • B01D71/26—Polyalkenes
    • B01D71/262—Polypropylene
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
    • B01D61/14—Ultrafiltration; Microfiltration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D69/00—Semi-permeable membranes for separation processes or apparatus characterised by their form, structure or properties; Manufacturing processes specially adapted therefor
    • B01D69/04—Tubular membranes
    • 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

Definitions

  • the present invention relates to a method for producing a polyhydroxyalkanoate aqueous dispersion having a concentration step by membrane separation.
  • Polyhydroxyalkanoate (hereinafter also referred to as PHA) is a thermoplastic polyester that is produced and accumulated as an energy storage substance in cells of many microbial species, and has biodegradability.
  • PHA Polyhydroxyalkanoate
  • non-petroleum-derived plastics are attracting attention due to increasing environmental awareness.
  • biodegradable plastics such as PHA, which are taken into the natural material cycle and whose decomposition products are not harmful, are receiving attention, and their practical application is earnestly desired.
  • PHA produced and accumulated by microorganisms in the cells is expected to have little adverse effect on the ecosystem because it is incorporated into the carbon cycle process in nature.
  • PHA is produced by a culture step of accumulating PHA in bacterial cells, a separation and purification step of recovering PHA from the bacterial cells, and a PHA drying step. Since the PHA aqueous dispersion obtained by the separation and purification process contains a large amount of water, it takes a long time and a large amount of energy is consumed in performing the drying process. As a method of reducing the time and energy required for drying, there is a method of concentrating the PHA aqueous dispersion after the separation and purification step. Examples of the method for concentrating the PHA aqueous dispersion include a method by centrifugation and a method by evaporation.
  • a cross-flow membrane separation method has been studied as a method capable of solving the above-mentioned problems when using a centrifugal separation method or an evaporation method (for example, see Patent Document 1).
  • Permeation flux and pressure loss become problems when the membrane separation process is used industrially. In industrial production, a high permeation flux is required to secure productivity. On the other hand, since high pressure deteriorates the membrane, operation at low pressure is required for long-term use of the membrane.
  • Patent Document 1 discloses a method including a step of subjecting a PHA suspension to tangential filtration, and a ceramic membrane or polymer membrane having an average pore size of 0.05 to 10 ⁇ m, preferably 0.2 to 5 ⁇ m. Is disclosed.
  • Patent Document 1 causes a significant decrease in permeation flux due to blockage of PHA particles, and a sharp increase in pressure due to an increase in viscosity of the PHA aqueous dispersion. It has been found that due to such a large increase, the PHA aqueous dispersion may not be concentrated to a high concentration of 50% by weight or more while maintaining a high permeation flux and a low pressure.
  • an object of the present invention is to provide a method for producing a PHA water dispersion liquid, which can obtain a concentrated PHA water dispersion liquid having a solid content concentration of more than 50% by weight, without significantly reducing the permeation flux and the pressure. To provide.
  • the present inventors have completed the present invention as a result of intensive studies for solving the above-mentioned problems.
  • the present invention provides the inventions according to the following [1] to [6], for example.
  • a method for producing an aqueous dispersion of polyhydroxyalkanoate wherein an aqueous dispersion of polyhydroxyalkanoate having a median diameter of polyhydroxyalkanoate particles of 1 to 5 ⁇ m and a solid content concentration of less than 50% by weight is used.
  • a process for producing an aqueous dispersion of polyhydroxyalkanoate which comprises the step of feeding the solution into a tubular membrane having a diameter of 4 to 10 mm and an average pore diameter of 0.05 to 0.5 ⁇ m to concentrate the solid content concentration to 50% by weight or more.
  • the PHA aqueous dispersion can be concentrated to a high concentration exceeding 50% by weight with high productivity by membrane separation.
  • the energy and time required for drying the PHA can be significantly reduced.
  • by lowering the pressure applied to the film it is possible to extend the life of the film.
  • 5 is a graph showing the solid content concentration of the PHA aqueous dispersion and the pressure loss of the membrane measured in Example 1 and Comparative Example 1.
  • 5 is a graph showing the solid content concentration of the PHA aqueous dispersion and the permeation flux of the membrane measured in Example 2 and Comparative Example 2. It is the schematic of the apparatus used for the concentration of the PHA aqueous dispersion in an Example.
  • the method for producing a PHA aqueous dispersion according to the present invention is a method for producing a PHA aqueous dispersion, which comprises the following step (a) of concentrating the PHA aqueous dispersion as an essential step.
  • the filtration method carried out by feeding the liquid into the tubular membrane in the step (a) is a cross flow method (a method in which the flow directions of the liquid to be filtered and the filtrate are orthogonal to each other), a dead end method (the liquid to be filtered and the filtrate).
  • the cross-flow method is preferable from the viewpoint of suppressing flow path clogging by PHA particles.
  • the PHA aqueous dispersion to be concentrated in step (a) of the method for producing a PHA aqueous dispersion of the present invention is an aqueous dispersion in which PHA particles are dispersed in water, and as described above, the median diameter of PHA particles is Is 1 to 5 ⁇ m and the solid content concentration is less than 50% by weight.
  • aqueous dispersion for example, a PHA obtained by producing PHA by a PHA-producing microorganism, and then chemically and / or physically and / or biologically treating the microorganism (PHA-containing bacterium) in water. It may be an aqueous dispersion. That is, the step (a) may be a step performed after culturing a PHA-producing microorganism (production of PHA) and separating and purifying PHA from the microorganism.
  • a method of solubilizing with a chemical such as an acid, an alkali, a surfactant, an organic solvent, or a cell wall synthesis inhibitor is preferable.
  • a chemical such as an acid, an alkali, a surfactant, an organic solvent, or a cell wall synthesis inhibitor.
  • a physical treatment for example, conventionally known French press, high-pressure homogenizer, X-press, ball mill, colloid mill, DYNO mill, ultrasonic homogenizer, fluid shear force, solid shear force, or grinding can be used.
  • a solution method is preferred.
  • a method using an enzyme such as lysozyme, pectinase, cellulase, thymolyase, and alcalase, and a crushing method of an autolysis method utilizing the action of protease or esterase contained in the cell itself are preferable.
  • the culture of PHA-producing microorganisms can be carried out according to a known or commonly used method and is not particularly limited. For example, it can be carried out by the method described in International Publication No. 2010/116681.
  • PHA contained in the PHA aqueous dispersion produced by the present invention has the following general formula (1): [-CHR-CH 2 -CO-O-] (1) (In the formula, R is an alkyl group represented by C n H 2n + 1 , and n is an integer of 1 or more and 15 or less.) It is preferable that it is at least one or more PHA containing the repeating unit shown by.
  • the PHA preferably contains the repeating unit represented by the general formula (1) in an amount of 50 mol% or more of all repeating units, and may further contain other repeating structures. In particular, it is more preferable that the repeating unit represented by the general formula (1) is contained in an amount of 70 mol% or more based on all the repeating units, and further preferably 80 mol% or more.
  • PHA examples include poly (3-hydroxybutyrate) (PHB), poly (3-hydroxybutyrate-co-3-hydroxyvalerate) (PHBV), and [poly (3-hydroxybutyrate-co- 3-hydroxyvalerate-co-3-hydroxyhexanoate) (P3HB3HV3HH), poly (3-hydroxybutyrate-co-3-hydroxyhexanoate) (PHBH), poly (3-hydroxybutyrate-co- 4-hydroxybutyrate) (P3HB4HB), poly (3-hydroxybutyrate-co-3-hydroxyoctanoate), poly (3-hydroxybutyrate-co-3-hydroxyoctadecanoate), poly (3 -Hydroxybutyrate-co-3-hydroxy-4-methylvalerate) (P3HB3H4MV) and the like.
  • PHB, PHBV, P3HB3HV3HH, PHBH, and P3HB4HB are particularly preferable because they are relatively easily industrially produced.
  • the average composition ratio of the repeating structural unit is 80 to 99 mol% from the viewpoint of the balance between flexibility and strength of PHA. Is preferred.
  • the PHA aqueous dispersion produced by the present invention may have one PHA alone or may have two or more PHA in combination.
  • the median diameter of PHA particles in the PHA aqueous dispersion to be concentrated in the step (a) is 1 to 5 ⁇ m, preferably 2 to 5 ⁇ m.
  • the median diameter is measured by the laser diffraction method.
  • the median diameter of PHA particles in the PHA aqueous dispersion can be adjusted by controlling the culture time, for example, when PHA is produced by culturing PHA-producing bacteria. For example, if the culture time is lengthened, the median diameter tends to increase.
  • the solid content concentration of the PHA aqueous dispersion to be concentrated in the step (a) is less than 50% by weight, and from the viewpoint of more effectively enjoying the effect of the present invention, preferably less than 45% by weight, more preferably It is less than 40% by weight, more preferably less than 35% by weight.
  • the lower limit of the solid content concentration is not particularly limited, but from the viewpoint of ensuring productivity, it is preferably 18% by weight or more, more preferably 20% by weight or more, and further preferably 25% by weight or more.
  • the PHA water dispersion liquid to be concentrated in the step (a) may contain water and other components other than PHA particles.
  • Other components include solvents other than water (for example, alcohols such as methanol, ethanol and ethylene glycol; ethers such as ethylene glycol monomethyl ether and ethylene glycol dimethyl ether), dispersants (for example, polyvinyl alcohol (PVA), Water-soluble polymers such as methyl cellulose, ethyl cellulose, hydroxymethyl cellulose, hydroxyethyl cellulose, polyacrylic acid, sodium polyacrylate, potassium polyacrylate, polymethacrylic acid, sodium polymethacrylate, etc., surfactants (eg sodium dodecyl sulfate) , Anionic surfactants such as sodium dodecylbenzenesulfonate, sodium cholate, sodium deoxycholate and sodium oleate; nonionic surfactants such as polyoxyethylene alkyl ethers and polyoxyalkylene alkyl ethers
  • Step (a) is a step of feeding the PHA aqueous dispersion into the tubular membrane (that is, filtering the PHA aqueous dispersion through the tubular membrane) and concentrating the aqueous dispersion.
  • the filtration using the tubular membrane is preferably filtration by a cross flow method (cross flow filtration).
  • Cross-flow filtration is a filtration method in which the treatment liquid has a relative velocity in the horizontal direction with respect to the membrane surface.
  • the average pore size of the tubular membrane which is the filtration membrane used in step (a), is 0.05 to 0.5 ⁇ m, more preferably 0.1 to 0.3 ⁇ m. If the average pore size of the tubular membrane is less than 0.05 ⁇ m, the permeation flux becomes low, and the membrane area required for industrial use becomes large, which increases costs and is not preferable. On the other hand, when the average pore diameter exceeds 0.5 ⁇ m, PHA particles enter the pores, the permeation flux is significantly reduced, and as a result, the required membrane area increases. Furthermore, it is not preferable because it becomes difficult to regenerate the film by washing and the cost increases in industrial use.
  • the average pore size of the tubular membrane is determined by the removal rate of inorganic particles whose average particle size is known.
  • the method for measuring the average pore diameter of a tubular membrane having an average pore diameter of 0.2 ⁇ m is as follows. Water was added to silica particles having an average particle diameter of 0.1 ⁇ m, and an aqueous dispersion of silica particles (test solution) at 200 mg / L was continuously introduced into the tubular membrane by a cross flow method with an inlet pressure of 0.03 MPa and a liquid temperature of room temperature. By passing the solution, the aqueous dispersion of silica particles is concentrated three times. Further, the same operation is performed on silica particles having an average particle diameter of 0.3 ⁇ m.
  • Removal rate (%) (1- (turbidity of filtrate / (turbidity of test liquid + turbidity of concentrated liquid) / 2)) ⁇ 100. If the removal rate of silica particles having an average particle size of 0.1 ⁇ m is 50% or less and the removal rate of silica particles having an average particle size of 0.3 ⁇ m is 95% or more, the average pore size of the tubular membrane is determined to be 0.2 ⁇ m.
  • the inner diameter of the tubular membrane is 4 to 10 mm, preferably 4 to 7 mm. If the inner diameter is less than 4 mm, the PHA aqueous dispersion whose viscosity has increased due to concentration tends to be clogged in the tubular membrane, making concentration impossible, which is not preferable. On the other hand, when the inner diameter exceeds 10 mm, the linear velocity applied to the film surface (the surface of the PHA particle layer formed on the film surface) decreases, so the force for peeling the PHA particle layer deposited on the film surface becomes weak and The PHA particle layer formed in the above becomes thick and the permeation flux becomes small, that is, the concentration time tends to increase. In addition, the number of membrane modules required increases, and the cost increases in industrial use, which is not preferable.
  • the inner diameter of the tubular membrane means the inner diameter of the circular hollow cross section of the tubular membrane.
  • the material of the tubular membrane (filtration membrane) is not particularly limited, but for example, polypropylene, fluororesin (eg, polytetrafluoroethylene, polyvinylidene fluoride, polyvinyl fluoride, tetrafluoroethylene / propylene hexafluoride copolymer) Polymer, ethylene / tetrafluoroethylene copolymer, etc.), cellulose ester (eg, cellulose acetate, cellulose acetate propionate, cellulose acetate butyrate, etc.), polysulfone resin (eg, polysulfone, polyether sulfone, etc.), poly Resins such as acrylonitrile and polyimide; porous ceramics such as alumina, mullite, zirconia, and cordierite; and inorganic materials such as porous bodies made of porous sintered metal such as stainless steel.
  • fluororesin eg, polytetrafluoroethylene, polyviny
  • step (a) the PHA aqueous dispersion is concentrated by passing it through the tubular membrane.
  • the filtration operation using the tubular membrane can be carried out by a known or common procedure.
  • the number of times the liquid is passed through the tubular membrane is not particularly limited, and usually, the PHA aqueous dispersion is concentrated by allowing the water to gradually permeate out of the tubular membrane by circulating the water inside the tubular membrane many times.
  • the transmembrane pressure difference when supplying the PHA aqueous dispersion to the tubular membrane is not particularly limited, but is preferably 0.001 to 0.1 MPa, and more preferably 0.01 to 0.1 MPa.
  • the transmembrane pressure difference is less than 0.001 MPa, the propulsive force required for filtration is insufficient and filtration is not performed, which is not preferable.
  • the transmembrane pressure difference exceeds 0.1 MPa, deterioration of the membrane due to the pressure tends to occur, which is not preferable.
  • the linear velocity at the time of concentrating the PHA aqueous dispersion is not particularly limited, but is preferably 1 to 5 m / s, more preferably 1.5 to 4 m / s, and further preferably Is 2 to 4 m / s.
  • the tubular film is made of resin (for example, polypropylene)
  • the upper limit of the linear velocity is preferably 3 m / s or less from the viewpoint of durability.
  • the pressure loss when concentrating the PHA aqueous dispersion is not particularly limited, but the pressure loss when concentrating the solid content concentration to 50% by weight is preferably 0.1 MPa or less, more preferably 0.05 MPa or less. Is. When it exceeds 0.1 MPa, the pressure tends to cause deterioration of the film, which is not preferable.
  • the permeation flux at the time of concentrating the PHA aqueous dispersion is not particularly limited, but the permeation flux at the time of concentrating the solid content concentration to 50% by weight is preferably 10 kg / m 2 ⁇ h or more, and more preferably Is 20 kg / m 2 ⁇ h or more. If it is less than 10 kg / m 2 ⁇ h, a large membrane area is required for industrial use, and the cost increases, which is not preferable.
  • a concentrated PHA aqueous dispersion is obtained.
  • the solid content concentration of the PHA aqueous dispersion obtained in step (a) is 50% by weight or more, preferably 52% by weight or more, more preferably 54% by weight or more.
  • the upper limit is not particularly limited, but from the viewpoint of securing the fluidity of the PHA aqueous dispersion, it is preferably 65% by weight or less, more preferably 60% by weight or less.
  • the method for producing a PHA water dispersion according to the present invention includes an additive (for example, the above-mentioned other components to the PHA water dispersion obtained in the step (a) other than the step (a). Component, etc.), a step of removing a part of water, etc.) may be included. Further, before the step (a), a step of culturing a PHA-producing bacterium, a step of obtaining a PHA aqueous dispersion from PHA-containing microbial cells obtained by the culturing (for example, a step of performing the above-mentioned separation and purification treatment, etc. ) May be included.
  • an additive for example, the above-mentioned other components to the PHA water dispersion obtained in the step (a) other than the step (a). Component, etc.
  • a step of removing a part of water, etc. may be included.
  • a step of culturing a PHA-producing bacterium a step
  • the PHA aqueous dispersion obtained by the method for producing a PHA aqueous dispersion of the present invention can be used as a raw material for various molded products such as films and coatings.
  • a solid PHA can be obtained by drying and removing water.
  • Example 1 The Ralstonia eutropha KNK-005 strain was cultured by the method described in Example 1 of WO 2010/116681 and contained poly (3-hydroxybutyrate-co-3-hydroxyhexanoate) (PHBH).
  • a cell culture solution was prepared.
  • the bacterial cell culture solution obtained above was sterilized by heating and stirring at an internal temperature of 60 to 80 ° C. for 20 minutes.
  • 0.2% by weight of sodium dodecyl sulfate was added to the sterilized cell culture solution obtained above.
  • an aqueous sodium hydroxide solution was added to adjust the pH to 11.0, and then the mixture was kept at 50 ° C. for 1 hour.
  • high-pressure crushing was performed using a high-pressure crusher (high-pressure homogenizer model PA2K type manufactured by Niro Soavi Co., Ltd.) at a pressure of 450 to 550 kgf / cm 2 .
  • An equal amount of distilled water was added to the crushed liquid obtained after high-pressure crushing. After centrifuging this, the supernatant was removed and concentrated twice.
  • the same amount of sodium hydroxide aqueous solution (pH 11) as the removed supernatant was added and centrifuged, and after removing the supernatant, water was added again to suspend.
  • PHBH aqueous dispersion having a median diameter of PHBH particles of 2 ⁇ m and a solid content concentration of 18% by weight (PHBH particle content: 180 g / L) was obtained.
  • the solution was circulated and supplied (delivered) at / s for concentration.
  • the PHA aqueous dispersion is concentrated by removing the filtrate from the tubular membrane 1 outside the system.
  • the pressure loss during concentration and the solid content concentration of the PHA aqueous dispersion after concentration were measured, and the results are shown in FIG. 1 together with the result of Comparative Example 1.
  • Example 1 the pressure loss was not significantly increased, the pressure loss could be 50 kPa or less, and the concentration to the solid content concentration of 50% by weight or more could be achieved while maintaining the low pressure.
  • the pressure loss was calculated by measuring the inlet pressure and the outlet pressure using pressure gauges 5 and 5 ′ installed at the inlet and the outlet of the tubular membrane 1 of FIG. 3, and subtracting the outlet pressure from the inlet pressure.
  • Pressure loss (inlet pressure)-(outlet pressure)
  • the solid content concentration was calculated by the following formula after measuring the weight of the PHA aqueous dispersion and then measuring the weight of PHA after removing water from the PHA aqueous dispersion.
  • Solid content concentration (wt%) (PHA weight) / (PHA aqueous dispersion weight) ⁇ 100
  • Example 1 The median diameter of PHBH particles was 2 ⁇ m in the same manner as in Example 1 except that the amount of water added last was changed using the cell culture solution obtained in the same manner as in Example 1.
  • the PHBH aqueous dispersion was placed in the tank 3, and circulated and supplied (liquid transfer) to a polypropylene hollow fiber membrane (MICRODYN R MD020CP2N) having an average pore diameter of 0.2 ⁇ m and an inner diameter of 1.8 mm at a linear velocity of 2 m / s, Concentration was carried out.
  • MICRODYN R MD020CP2N polypropylene hollow fiber membrane having an average pore diameter of 0.2 ⁇ m and an inner diameter of 1.8 mm at a linear velocity of 2 m / s
  • Example 2 Using the bacterial cell culture solution obtained by the same method as in Example 1, the median diameter of PHBH particles was 2 ⁇ m and the solid content concentration was 18% by weight (the content of PHBH particles was the same as in Example 1). : 180 g / L) to obtain a PHBH aqueous dispersion.
  • the PHBH aqueous dispersion is charged into a tank 3, and is circulated and supplied (liquid transfer) at a linear velocity of 2 m / s to a polypropylene tubular membrane (MICRODYN R MD020TP2N) having an average pore diameter of 0.2 ⁇ m and an inner diameter of 5.5 mm, and concentrated. was carried out.
  • MICRODYN R MD020TP2N polypropylene tubular membrane having an average pore diameter of 0.2 ⁇ m and an inner diameter of 5.5 mm
  • Example 2 The permeation flux at the time of concentration and the solid content concentration of the PHA aqueous dispersion after concentration were measured, and the results are shown together with the result of Comparative Example 2 in FIG. From this, in Example 2, it was possible to achieve concentration to a solid content concentration of 50% by weight or more while maintaining the permeation flux at 10 kg / m 2 ⁇ h or more.
  • the permeation flux was calculated by measuring the permeation liquid (PHA water dispersion liquid) for 1 minute and dividing it by the membrane area. Further, the solid content concentration was calculated by the above-described method and formula.
  • Example 2 The median diameter of PHBH particles was 2 ⁇ m in the same manner as in Example 1 except that the amount of water added last was changed using the cell culture solution obtained in the same manner as in Example 1.
  • a PHBH aqueous dispersion having a solid content concentration of 10% by weight (PHBH particle content: 100 g / L) was obtained.
  • Put the PHBH aqueous dispersion tank 3, and an average pore diameter 1.0 .mu.m, circulated and supplied into a polyethylene tubular film having an inner diameter of 5mm (SEPRODYN R SE020TP1N) at a linear velocity of 2m / s (liquid feed), carried out concentrated did.

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Abstract

L'invention concerne un procédé de production d'une dispersion aqueuse de polyhydroxyalcanoate, le procédé comprenant une étape dans laquelle une dispersion aqueuse de polyhydroxyalcanoate contenant des particules de polyhydroxyalcanoate ayant un diamètre médian de 1 à 5 µm et ayant une concentration en solides inférieure à 50% en poids est envoyé dans une membrane tubulaire ayant un diamètre interne de 4 à 10 mm et un diamètre de pore moyen de 0,05 à 0,5 µm pour augmenter la concentration solide à 50% en poids ou plus.
PCT/JP2019/042634 2018-11-12 2019-10-30 Procédé de production d'une dispersion aqueuse de polyhydroxyalcanoate Ceased WO2020100598A1 (fr)

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JPWO2021079750A1 (fr) * 2019-10-25 2021-04-29
JP2022175471A (ja) * 2021-05-13 2022-11-25 株式会社カネカ ろ過膜の薬剤洗浄時期の予測方法およびその利用
US20230220155A1 (en) * 2022-01-12 2023-07-13 Meredian, Inc. Aqueous coatings made from polyhydroxyalkanoate (pha) cake
JP2024527799A (ja) * 2021-07-30 2024-07-26 シージェイ チェイルジェダン コーポレーション ポリヒドロキシアルカノエート（ｐｈａ）分散液及びその調製方法

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Cited By (7)

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JPWO2021079750A1 (fr) * 2019-10-25 2021-04-29
WO2021079750A1 (fr) * 2019-10-25 2021-04-29 株式会社カネカ Procédé de production de dispersion aqueuse de polymère
JP7595022B2 (ja) 2019-10-25 2024-12-05 株式会社カネカ ポリマー水分散液の製造方法
JP2022175471A (ja) * 2021-05-13 2022-11-25 株式会社カネカ ろ過膜の薬剤洗浄時期の予測方法およびその利用
JP2024527799A (ja) * 2021-07-30 2024-07-26 シージェイ チェイルジェダン コーポレーション ポリヒドロキシアルカノエート（ｐｈａ）分散液及びその調製方法
US20230220155A1 (en) * 2022-01-12 2023-07-13 Meredian, Inc. Aqueous coatings made from polyhydroxyalkanoate (pha) cake
JP2025503341A (ja) * 2022-01-12 2025-02-03 ダニマー・アイピーシーオー・エルエルシー ポリヒドロキシアルカノエート（ｐｈａ）ケーキから作製される水性コーティング

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