WO2012014900A1 - スチーム選択透過膜、及びこれを用いてスチームを混合ガスから分離する方法 - Google Patents
スチーム選択透過膜、及びこれを用いてスチームを混合ガスから分離する方法 Download PDFInfo
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- WO2012014900A1 WO2012014900A1 PCT/JP2011/066983 JP2011066983W WO2012014900A1 WO 2012014900 A1 WO2012014900 A1 WO 2012014900A1 JP 2011066983 W JP2011066983 W JP 2011066983W WO 2012014900 A1 WO2012014900 A1 WO 2012014900A1
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- steam
- membrane
- compound
- mixed gas
- alkali metal
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- 239000012528 membrane Substances 0.000 title claims abstract description 170
- 238000000034 method Methods 0.000 title claims description 21
- 229920001477 hydrophilic polymer Polymers 0.000 claims abstract description 40
- 150000001339 alkali metal compounds Chemical class 0.000 claims abstract description 28
- -1 cesium compound Chemical class 0.000 claims abstract description 17
- 229910052792 caesium Inorganic materials 0.000 claims abstract description 15
- 150000003112 potassium compounds Chemical class 0.000 claims abstract description 11
- 150000003298 rubidium compounds Chemical class 0.000 claims abstract description 11
- 239000012466 permeate Substances 0.000 claims description 12
- ZLMJMSJWJFRBEC-UHFFFAOYSA-N Potassium Chemical compound [K] ZLMJMSJWJFRBEC-UHFFFAOYSA-N 0.000 claims description 4
- TVFDJXOCXUVLDH-UHFFFAOYSA-N caesium atom Chemical compound [Cs] TVFDJXOCXUVLDH-UHFFFAOYSA-N 0.000 claims description 4
- 229910052700 potassium Inorganic materials 0.000 claims description 4
- 239000011591 potassium Substances 0.000 claims description 4
- 229910052701 rubidium Inorganic materials 0.000 claims description 4
- IGLNJRXAVVLDKE-UHFFFAOYSA-N rubidium atom Chemical compound [Rb] IGLNJRXAVVLDKE-UHFFFAOYSA-N 0.000 claims description 4
- 239000007789 gas Substances 0.000 description 69
- 229920001343 polytetrafluoroethylene Polymers 0.000 description 33
- 239000004810 polytetrafluoroethylene Substances 0.000 description 33
- HUCVOHYBFXVBRW-UHFFFAOYSA-M caesium hydroxide Chemical compound [OH-].[Cs+] HUCVOHYBFXVBRW-UHFFFAOYSA-M 0.000 description 32
- 239000000499 gel Substances 0.000 description 27
- 239000000243 solution Substances 0.000 description 24
- 230000002209 hydrophobic effect Effects 0.000 description 20
- 239000004372 Polyvinyl alcohol Substances 0.000 description 15
- 229920002451 polyvinyl alcohol Polymers 0.000 description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 9
- 229920001577 copolymer Polymers 0.000 description 7
- SXRSQZLOMIGNAQ-UHFFFAOYSA-N Glutaraldehyde Chemical compound O=CCCCC=O SXRSQZLOMIGNAQ-UHFFFAOYSA-N 0.000 description 6
- AIYUHDOJVYHVIT-UHFFFAOYSA-M caesium chloride Chemical compound [Cl-].[Cs+] AIYUHDOJVYHVIT-UHFFFAOYSA-M 0.000 description 6
- 238000005266 casting Methods 0.000 description 6
- 238000011156 evaluation Methods 0.000 description 6
- 239000011521 glass Substances 0.000 description 6
- CPRMKOQKXYSDML-UHFFFAOYSA-M rubidium hydroxide Chemical compound [OH-].[Rb+] CPRMKOQKXYSDML-UHFFFAOYSA-M 0.000 description 6
- 239000007864 aqueous solution Substances 0.000 description 5
- 238000001816 cooling Methods 0.000 description 4
- 239000000017 hydrogel Substances 0.000 description 4
- WSFSSNUMVMOOMR-UHFFFAOYSA-N Formaldehyde Chemical compound O=C WSFSSNUMVMOOMR-UHFFFAOYSA-N 0.000 description 3
- 229920002125 Sokalan® Polymers 0.000 description 3
- 229910052783 alkali metal Inorganic materials 0.000 description 3
- 150000001340 alkali metals Chemical class 0.000 description 3
- 239000000969 carrier Substances 0.000 description 3
- 150000001875 compounds Chemical class 0.000 description 3
- 238000001035 drying Methods 0.000 description 3
- 238000010438 heat treatment Methods 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000035699 permeability Effects 0.000 description 3
- 229920001661 Chitosan Polymers 0.000 description 2
- PNEYBMLMFCGWSK-UHFFFAOYSA-N aluminium oxide Inorganic materials [O-2].[O-2].[O-2].[Al+3].[Al+3] PNEYBMLMFCGWSK-UHFFFAOYSA-N 0.000 description 2
- 239000000919 ceramic Substances 0.000 description 2
- 238000010382 chemical cross-linking Methods 0.000 description 2
- 230000000052 comparative effect Effects 0.000 description 2
- 238000004132 cross linking Methods 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 150000002642 lithium compounds Chemical class 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 230000002093 peripheral effect Effects 0.000 description 2
- 229920000083 poly(allylamine) Polymers 0.000 description 2
- 239000004584 polyacrylic acid Substances 0.000 description 2
- 229920000036 polyvinylpyrrolidone Polymers 0.000 description 2
- 239000001267 polyvinylpyrrolidone Substances 0.000 description 2
- 235000013855 polyvinylpyrrolidone Nutrition 0.000 description 2
- 239000002994 raw material Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 150000003388 sodium compounds Chemical class 0.000 description 2
- QTBSBXVTEAMEQO-UHFFFAOYSA-M Acetate Chemical compound CC([O-])=O QTBSBXVTEAMEQO-UHFFFAOYSA-M 0.000 description 1
- BVKZGUZCCUSVTD-UHFFFAOYSA-L Carbonate Chemical compound [O-]C([O-])=O BVKZGUZCCUSVTD-UHFFFAOYSA-L 0.000 description 1
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- 150000008044 alkali metal hydroxides Chemical class 0.000 description 1
- 230000005540 biological transmission Effects 0.000 description 1
- 150000007942 carboxylates Chemical class 0.000 description 1
- 239000003431 cross linking reagent Substances 0.000 description 1
- 238000007791 dehumidification Methods 0.000 description 1
- 238000004817 gas chromatography Methods 0.000 description 1
- 150000002484 inorganic compounds Chemical class 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 238000010030 laminating Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052751 metal Inorganic materials 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 238000000465 moulding Methods 0.000 description 1
- 150000002902 organometallic compounds Chemical class 0.000 description 1
- 229920000058 polyacrylate Polymers 0.000 description 1
- 230000008961 swelling Effects 0.000 description 1
- 229920002554 vinyl polymer Polymers 0.000 description 1
Images
Classifications
-
- 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
-
- 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
- B01D71/30—Polyalkenyl halides
- B01D71/32—Polyalkenyl halides containing fluorine atoms
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/22—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion
- B01D53/228—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by diffusion characterised by specific membranes
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/26—Drying gases or vapours
- B01D53/268—Drying gases or vapours by diffusion
-
- 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
- B01D61/36—Pervaporation; Membrane distillation; Liquid permeation
- B01D61/363—Vapour permeation
-
- 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
- B01D69/14—Dynamic membranes
- B01D69/141—Heterogeneous membranes, e.g. containing dispersed material; Mixed matrix membranes
- B01D69/142—Heterogeneous membranes, e.g. containing dispersed material; Mixed matrix membranes with "carriers"
-
- 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
- B01D71/02—Inorganic material
-
- 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
- B01D71/76—Macromolecular material not specifically provided for in a single one of groups B01D71/08 - B01D71/74
- B01D71/82—Macromolecular material not specifically provided for in a single one of groups B01D71/08 - B01D71/74 characterised by the presence of specified groups, e.g. introduced by chemical after-treatment
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2256/00—Main component in the product gas stream after treatment
- B01D2256/22—Carbon dioxide
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2257/00—Components to be removed
- B01D2257/80—Water
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D2323/00—Details relating to membrane preparation
- B01D2323/30—Cross-linking
Definitions
- the present invention relates to a steam permselective membrane and a method for separating steam from a mixed gas using the same.
- Patent Literature As a method for selectively separating steam from a mixed gas containing steam, a method has been proposed in which a separation membrane having a gel layer manufactured from a metal organic compound or a metal inorganic compound is used as a steam selective permeable membrane (Patent Literature). 1).
- an object of the present invention is to provide a steam permselective membrane that can permeate steam with high permeation speed and high selectivity.
- the steam permselective membrane according to the present invention contains a crosslinked hydrophilic polymer.
- the steam permselective membrane preferably further contains an alkali metal compound.
- the steam permselective membrane according to the present invention may contain a hydrophilic polymer and an alkali metal compound.
- the steam permselective membrane according to the present invention it is possible to permeate steam with a high permeation rate and high selectivity.
- the alkali metal compound may contain at least one selected from the group consisting of a cesium compound, a potassium compound and a rubidium compound.
- the concentration of cesium based on the total mass of the hydrophilic polymer and the alkali metal compound may be 0.003 mol / g or less.
- the alkali metal compound includes a potassium compound and / or a rubidium compound, the total concentration of potassium and rubidium based on the total mass of the hydrophilic polymer and the alkali metal compound may be 0.005 mol / g or less.
- the present invention relates to a method for separating steam from a mixed gas.
- the method according to the present invention comprises the step of separating steam from the mixed gas by allowing the steam permeation membrane according to the present invention to permeate steam in the mixed gas containing steam.
- the steam permeation membrane according to the present invention permeate steam in the mixed gas containing steam.
- the partial pressure of steam on the other surface side of the steam permselective membrane can be made lower than the partial pressure of steam in the mixed gas without substantially using a sweep gas.
- the steam permselective membrane according to the present invention can permeate steam at a high permeation rate and high selectivity.
- the steam permselective membrane of the present invention can exhibit a high permeation rate and selectivity even at a high temperature exceeding 100 ° C.
- the steam permselective membrane according to the present invention is an organic membrane, and has advantages such as easy molding and low cost per membrane area as compared with an inorganic membrane.
- Relationship between the steam permeance and temperature and is a graph showing the relationship between the steam / CO 2 selectivity and Cs concentration. Relationship between the steam permeance and temperature, and is a graph showing the relationship between the steam / CO 2 selectivity and Cs concentration. Relationship between the steam permeance and temperature, and is a graph showing the relationship between the steam / CO 2 selectivity and Cs concentration. Relationship between the steam permeance and temperature, and is a graph showing the relationship between the steam / CO 2 selectivity and K concentrations. Relationship between the steam permeance and temperature, and is a graph showing the relationship between the steam / CO 2 selectivity and K concentrations.
- Relationship between the steam permeance and temperature and is a graph showing the relationship between the steam / CO 2 selectivity and Rb concentrations.
- Relationship between the steam permeance and temperature and is a graph showing the relationship between the steam / CO 2 selectivity and Rb concentrations.
- Relationship between the steam permeance and Feed side pressure and is a graph showing the relationship between the steam / CO 2 selectivity and Feed side pressure.
- FIG. 1 is a cross-sectional view showing an embodiment of a membrane laminate including a steam permselective membrane.
- a membrane laminate 10 shown in FIG. 1 includes a steam selective permeable membrane 1 and porous membranes 2 a and 2 b provided on both sides of the steam selective permeable membrane 1.
- the steam permselective membrane 1 has a gel-like hydrophilic polymer layer containing a crosslinked hydrophilic polymer.
- the hydrophilic polymer layer is a hydrogel in which a hydrophilic polymer is crosslinked to form a three-dimensional network structure. Hydrogels often have the property of swelling by absorbing water.
- the hydrophilic polymer is selected from, for example, polyvinyl alcohol-polyacrylate copolymer (PVA-PAA salt copolymer), polyvinyl alcohol, polyacrylic acid, chitosan, polyvinylamine, polyallylamine, and polyvinylpyrrolidone.
- the degree of crosslinking of the hydrogel of PVA-PAA salt copolymer and the hydrogel of polyvinyl alcohol can be further controlled by a dialdehyde compound such as glutaraldehyde and / or an aldehyde compound such as formaldehyde.
- a dialdehyde compound such as glutaraldehyde and / or an aldehyde compound such as formaldehyde.
- the PVA-PAA salt copolymer is sometimes referred to as a PVA-PAA copolymer.
- the hydrophilic polymer layer preferably contains at least one alkali metal compound selected from the group consisting of a cesium compound, a potassium compound and a rubidium compound.
- This alkali metal compound functions as a carrier that promotes selective permeation of moisture.
- the alkali metal compound is, for example, an alkali metal hydroxide, carbonate, nitrate, carboxylate (acetate, etc.) or chloride selected from cesium (Cs), potassium (K), and rubidium (Rb).
- the hydrophilic polymer layer may further contain a lithium compound and / or a sodium compound in addition to an alkali metal compound selected from a cesium compound, a potassium compound and a rubidium compound.
- the concentration of cesium based on the total mass of the hydrophilic polymer and the alkali metal compound is preferably 0.003 mol / g or less.
- the alkali metal compound contains a potassium compound and / or a rubidium compound
- the total concentration of potassium and rubidium based on the total mass of the hydrophilic polymer and the alkali metal compound is preferably 0.005 mol / g or less.
- the lower limit of the concentration of at least one alkali metal selected from the group consisting of a cesium compound, a potassium compound and a rubidium compound is not particularly limited, but is preferably 0.001 based on the total mass of the hydrophilic polymer and the alkali metal compound. It is at least mol / g.
- the steam permselective membrane 1 may have a hydrophilic polymer layer containing an uncrosslinked hydrophilic polymer and at least one alkali metal compound selected from the group consisting of a cesium compound, a potassium compound and a rubidium compound. Good.
- the hydrophilic polymer used in this case is selected from, for example, polyvinyl alcohol, polyacrylic acid, chitosan, polyvinylamine, polyallylamine, and polyvinylpyrrolidone.
- the alkali metal compound the same ones as described above can be used.
- the preferable concentration range of the alkali metal is the same as described above.
- the steam permselective membrane 1 is preferably composed of the hydrophilic polymer layer and a porous membrane, and at least a part of the hydrophilic polymer layer is preferably filled in the porous membrane.
- This porous membrane is preferably hydrophilic.
- the hydrophilic porous membrane include a hydrophilized polytetrafluoroethylene porous membrane (hydrophilic PTFE porous membrane) and a hydrophilic ceramic porous membrane (alumina porous membrane, etc.).
- the porous membranes 2a and 2b are preferably hydrophobic.
- the hydrophobic porous membrane include a polytetrafluoroethylene porous membrane (hydrophobic PTFE porous membrane) that has not been made hydrophilic.
- the porous membranes 2a and 2b are not necessarily provided.
- the film laminate 10 is formed, for example, by preparing a cast solution containing a hydrophilic polymer and, if necessary, an alkali metal compound and water in which they are dissolved, and a film of the cast solution on one porous film 2a. It can be produced by a method comprising a step, a step of drying a cast solution membrane to form a hydrophilic polymer layer, and a step of providing the other porous membrane 2b on the hydrophilic polymer layer.
- the cast solution can be prepared by dissolving a hydrophilic polymer and an alkali metal compound in water.
- the hydrophilic polymer can be chemically crosslinked by adding a crosslinking agent such as glutaraldehyde to the cast solution.
- the casting solution is heated as necessary to allow the crosslinking of the hydrophilic polymer to proceed.
- Cast film can be cast to form a cast solution film. Casting can be performed by an ordinary method using an applicator or the like. By placing a hydrophilic porous film on the hydrophobic porous film 2a and casting the cast solution on the hydrophilic porous film, a part of the cast solution is filled into the hydrophilic porous film.
- the gel-like hydrophilic polymer layer is formed by removing water from the cast solution film. Thereafter, the hydrophilic polymer may be further crosslinked by heating.
- the membrane laminate 10 is obtained by laminating the porous membrane 2b on the steam selective permeable membrane 1 having a hydrophilic polymer layer.
- the film laminate according to the present embodiment can be used for separating steam from a mixed gas containing steam and other gases.
- a mixed gas containing steam is supplied to the porous membrane 2a side (Feed side), and the steam selectively permeable membrane 1 is permeated through the steam, and the permeated steam is separated to the porous membrane 2b side.
- the steam can be efficiently transmitted to the steam permselective membrane 1 Can be transmitted through.
- a sweep gas such as Ar gas may be continuously supplied to the porous film 2b side.
- the steam recovered from the mixed gas is reused, it is preferable to adjust the steam partial pressure difference without substantially using the sweep gas.
- the partial pressure difference of the steam can be adjusted by a method such as making the total pressure on the porous membrane 2a side higher than the total pressure on the porous membrane 2b side.
- the steam permselective membrane 1 can also be used for purposes other than the reuse of steam, such as dehumidification of a mixed gas.
- the steam permselective membrane 1 When permeating steam, the steam permselective membrane 1 is preferably heated to 100 to 200 ° C.
- the steam permselective membrane according to this embodiment can exhibit high steam permeability and high steam selectivity even at such a high temperature. Therefore, high-temperature steam can be recovered and reused without being liquefied by cooling. According to this method, compared with the case where water liquefied by cooling is heated again and reused as steam, the latent heat of steam can be used more effectively, so that higher energy efficiency can be realized.
- transmitted the steam selective permeable membrane is not reused as steam, the recovered steam may be liquefied by cooling and recovered.
- the steam permselective membrane 1 is particularly preferably used for separating steam from a mixed gas containing steam and CO 2 .
- the steam permselective membrane 1 is particularly preferably used for separating steam from a mixed gas containing steam and CO 2 .
- the method employing a combination of can be recovered CO 2 at high energy efficiency from a gas containing CO 2.
- the steam permselective membrane is not limited to the embodiment described above, and can be appropriately modified without departing from the gist of the present invention.
- the steam permselective membrane may be formed in a cylindrical shape.
- FIG. 2 is a cross-sectional view showing an embodiment of a gas processing apparatus provided with a cylindrical steam selective permeable membrane.
- 2A shows a cross section perpendicular to the longitudinal direction of the gas processing apparatus
- FIG. 2B shows a cross section parallel to the longitudinal direction of the gas processing apparatus.
- a gas processing apparatus 20 shown in FIG. 2 includes a cylindrical steam permselective membrane 1 and a cylindrical container 5 that accommodates the steam permselective membrane 1.
- the steam permselective membrane 1 is composed of a cylindrical hydrophilic polymer layer 3 and a cylindrical porous membrane 4 provided on the inside thereof. A part of the hydrophilic polymer layer 3 is filled in the porous film 4.
- the hydrophilic polymer layer 3 may be supported on the inner peripheral surface side of the porous film 4.
- the cross-sectional shape of the cylindrical steam permselective membrane does not necessarily have to be a perfect circle, and can be deformed to an arbitrary shape such as an ellipse.
- the container 5 and the steam permselective membrane 1 are divided into the space 11 on the Feed side into which the mixed gas 30 containing steam flows and the steam permeated through the steam permselective membrane 1. And the space 12 on the sweep side containing the exhaust gas 35 containing the.
- the container 5 is provided with an opening 21 provided at one end for allowing the feed-side space 11 to communicate with the outside of the container 5, and a feed-side space 11 provided at the other end for the outside of the container 5. And an opening 25 for communicating the space 12 on the side of the sweep to the outside of the container 5.
- the mixed gas 30 is supplied from the opening 21 to the space 11 on the Feed side and is discharged from the opening 22.
- the steam that permeates the steam selective permeable membrane 1 and is separated from the mixed gas 30 is collected in the exhaust gas 35 that is discharged from the opening 25. Steam gas may be flowed into the space 12 on the sweep side in the same manner as described above.
- a hydrophobic PTFE porous membrane (Sumitomo Electric, Fluoropore FP-010) was placed on a glass plate, and a hydrophilic PTFE porous membrane (Sumitomo Electric, WPW-020-80) was placed thereon.
- the cast solution was cast to a thickness of 500 ⁇ m using a Baker applicator. At this time, a part of the cast solution was filled in the hydrophilic PTFE porous membrane. Thereafter, the cast casting solution was dried for about 12 hours in a dry box maintained at a humidity of about 5% to form a gel layer. After drying, the formed gel layer was placed in a thermostat kept at 120 ° C.
- a steam selective permeable membrane composed of a hydrophilic PTFE porous membrane and a gel layer.
- a hydrophobic PTFE porous membrane was laminated on the steam selective permeable membrane to obtain a membrane laminate having a three-layer structure of hydrophobic PTFE porous membrane / steam selective permeable membrane / hydrophobic PTFE porous membrane.
- PVA-PAA salt copolymer / CsOH 2.0 g of PVA-PAA salt copolymer (SS gel) was dissolved in 80.0 g of ion-exchanged water at room temperature. 0.064g of 25 mass% glutaraldehyde aqueous solution was added to the obtained SS gel aqueous solution. Subsequently, the solution was heated at 95 ° C. for 12 hours to allow chemical crosslinking with glutaraldehyde to proceed. Thereafter, CsOH was added as a carrier and dissolved to obtain a cast solution. The amount of CsOH was adjusted such that the concentration of CsOH with respect to the total mass of SS gel and CsOH was 30% by mass. At this time, the molar concentration of Cs is 0.002 mol / g based on the total mass of SS gel and CsOH.
- a hydrophobic PTFE porous membrane (Sumitomo Electric, Fluoropore FP-010) was placed on a glass plate, and a hydrophilic PTFE porous membrane (Sumitomo Electric, WPW-020-80) was placed thereon.
- the cast solution was cast to a thickness of 500 ⁇ m using a Baker applicator. Thereafter, the cast casting solution was dried for about 12 hours in a dry box maintained at a humidity of about 5% to form a gel layer. After drying, the formed gel layer was placed in a thermostat kept at 120 ° C.
- a steam selective permeable membrane composed of a hydrophilic PTFE porous membrane and a gel layer.
- a hydrophobic PTFE porous membrane was laminated on the steam selective permeable membrane to obtain a membrane laminate having a three-layer structure of hydrophobic PTFE porous membrane / steam selective permeable membrane / hydrophobic PTFE porous membrane.
- a hydrophobic PTFE porous membrane (Sumitomo Electric, Fluoropore FP-010) was placed on a glass plate, and a hydrophilic PTFE porous membrane (Sumitomo Electric, WPW-020-80) was placed thereon.
- the cast solution was cast to a thickness of 500 ⁇ m using a Baker applicator. Thereafter, the cast casting solution was dried for about 12 hours in a dry box maintained at a humidity of about 5% to form a steam selective permeable membrane composed of a hydrophilic PTFE porous membrane and a PVA layer. .
- hydrophobic PTFE porous membrane was laminated on the steam selective permeable membrane to obtain a membrane laminate having a three-layer structure of hydrophobic PTFE porous membrane / steam selective permeable membrane / hydrophobic PTFE porous membrane.
- PVA comparative membrane
- a hydrophobic PTFE porous membrane (Sumitomo Electric Fluoropore FP-010) was placed on a glass plate, and a hydrophilic PTFE porous membrane (Sumitomo Electric WPW-020-80) was placed thereon.
- a 5 mass% PVA aqueous solution was cast so as to have a thickness of 500 ⁇ m using a Baker applicator. Thereafter, the cast aqueous PVA solution was dried for about 12 hours in a dry box maintained at a humidity of about 5% to form a steam selective permeable membrane composed of a hydrophilic PTFE porous membrane and a PVA layer.
- hydrophobic PTFE porous membrane was laminated on the steam selective permeable membrane to obtain a membrane laminate having a three-layer structure of hydrophobic PTFE porous membrane / steam selective permeable membrane / hydrophobic PTFE porous membrane.
- the membrane laminate was attached to a membrane evaluation apparatus, and gas permeation performance was evaluated. While heating the film stack to a predetermined temperature, a raw material gas containing CO 2 , N 2 and H 2 O (steam) is supplied to one surface side (Feed side) of the film stack, opposite to the Feed side. Ar gas as a sweep gas was allowed to flow on the side (Sweep side). A membrane that is an index of the steam permeation rate based on the amount of water collected from the exhaust gas containing Ar gas and gas permeated from the Feed side to the Sweep side by recovering water with a cooling trap. The steam permeance [mol / (m 2 ⁇ s ⁇ kPa)] was calculated.
- the composition of the remaining exhaust gas was quantified by gas chromatography, and the CO 2 permeance [mol / (m 2 ⁇ s ⁇ kPa)] of the membrane was calculated from the result and the Ar gas flow rate. Furthermore, the ratio of steam permeance for CO 2 permeance (the steam permeance / CO 2 permeance) was calculated as the selectivity of the steam transmission for CO 2 permeability (steam / CO 2 selectivity).
- the evaluation conditions for gas permeation performance are shown in the following table.
- FIG. 3 is a graph showing the relationship between steam permeance and temperature and the relationship between steam / CO 2 selectivity and temperature for each membrane of SS gel only, SS gel / CsOH, PVA / CsOH, and PVA only.
- the membrane using SS gel showed particularly high steam / CO 2 selectivity in a high temperature region.
- Example 2 Production of a membrane laminate including a steam selective permeable membrane Using CsOH, Cs 2 CO 3 , CsNO 3 , CH 3 COOCs or CsCl as a carrier, a steam selection containing a carrier having the concentrations shown in the following tables and an SS gel A membrane laminate including a permeable membrane was produced in the same procedure as in Study 1.
- Cs concentration is the ratio of the number of moles of Cs to the total mass (g) of SS gel and carrier (CsOH)
- the carrier concentration is the ratio of the mass of carrier to the total mass of SS gel and carrier.
- FIG. 13 is a graph showing the relationship between steam permeance and Feed side pressure, and the relationship between steam / CO 2 selectivity and Feed side pressure. As shown in FIG. 13, it is confirmed that a high steam permeance and steam / CO 2 selectivity can be obtained by providing a difference in steam partial pressure between the Feed side and the Sweep side without using a sweep gas. It was done.
- Example 5 An apparatus having the same configuration as the gas processing apparatus shown in FIG. 2 was prepared.
- a cylindrical ceramic porous film (alumina porous film) was used as the porous film 4, and a hydrophilic polymer layer 3 containing SS gel and CsCl as a carrier was supported on the outer peripheral surface thereof.
- the carrier concentration was 15% by mass.
- gas permeation performance was evaluated under the conditions shown in the following table.
- the CO 2 flow rate and Ar flow rate in the table are shown as volume flow rates of 25 ° C. and 1 atm.
- H 2 O supply amount was shown as the supply amount of of H 2 O liquid. Liquid H 2 O was vaporized by heating, and a gas mixture of vaporized H 2 O and CO 2 was supplied to the Feed side.
- the steam fraction of the mixed gas was 82%.
- the pressures shown in the table are absolute pressures.
- the steam permeance was 3.1 ⁇ 10 ⁇ 3 [mol / (m 2 ⁇ s ⁇ kPa)], and the steam / CO 2 selectivity was 2.9 ⁇ 10 3 . From this result, it was confirmed that the cylindrical steam selective permeable membrane also has very excellent steam permeability and steam / CO 2 selectivity.
- the steam permselective membrane according to the present invention can be used for selectively separating steam from a mixed gas containing steam.
- SYMBOLS 1 Steam selective permeable membrane, 2a, 2b ... Porous membrane, 3 ... Hydrophilic polymer, 4 ... Porous membrane of a layer steam selective permeable membrane, 10 ... Membrane laminated body, 20 ... Gas processing apparatus, 30 ... Mixed gas containing steam .
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Abstract
Description
1.スチーム選択透過膜を含む膜積層体の作製
(1)PVA-PAA塩共重合体
PVA-PAA塩共重合体(住友精化製、以下「SSゲル」という。)2.0gを室温でイオン交換水80.0gに溶解させた。得られたSSゲル溶液に、25質量%のグルタルアルデヒド水溶液を0.064g加えた。続いて、溶液を95℃で12時間加熱して、グルタルアルデヒドによる化学的な架橋を進行させて、キャスト溶液を得た。
PVA-PAA塩共重合体(SSゲル)2.0gを室温でイオン交換水80.0gに溶解させた。得られたSSゲル水溶液に、25質量%のグルタルアルデヒド水溶液を0.064g加えた。続いて、溶液を95℃で12時間加熱して、グルタルアルデヒドによる化学的な架橋を進行させた。その後、キャリアとしてCsOHを加え、それを溶解させて、キャスト溶液を得た。CsOHの量は、SSゲル及びCsOHの合計質量に対するCsOHの濃度が30質量%となるように調整した。このとき、Csのモル濃度はSSゲル及びCsOHの合計質量を基準として0.002モル/gである。
5質量%のPVA水溶液10.25gに、キャリアとしてのCsOH0.219gを溶解させて、キャスト溶液を得た。このとき、Csのモル濃度はPVA及びCsOHの合計質量を基準として0.002モル/gである。
ガラス板に疎水性PTFE多孔膜(住友電工製、Fluoropore FP-010)を載せ、その上に親水性PTFE多孔膜(住友電工製、WPW-020-80)を載せた。親水性PTFE多孔膜上に、ベーカーアプリケーターを用いて、5質量%のPVA水溶液を厚み500μmとなるようにキャストした。その後、キャストされたPVA水溶液を湿度が約5%に保たれたドライボックス内で約12時間かけて乾燥させて、親水性PTFE多孔膜及びPVA層から構成されるスチーム選択透過膜を形成させた。さらに、スチーム選択透過膜の上に疎水性PTFE多孔膜を積層して、疎水性PTFE多孔膜/スチーム選択透過膜/疎水性PTFE多孔膜の3層構成を有する膜積層体を得た。
膜積層体をメンブレン評価装置に取り付け、ガス透過性能の評価を行った。膜積層体を所定の温度に加熱しながら、膜積層体の一方の面側(Feed側)にCO2、N2及びH2O(スチーム)を含む原料ガスを供給し、Feed側とは反対側(Sweep側)にスイープガスとしてのArガスを流した。Feed側からSweep側に透過したガス及びArガスを含む排出ガスから、冷却トラップにより水を回収してその量を一定時間毎に定量し、その量に基づいて、スチーム透過速度の指標である膜のスチームパーミアンス[mol/(m2・s・kPa)]を計算した。残りの排出ガスの組成をガスクロマトグラフィーにより定量し、その結果とArガス流量から膜のCO2パーミアンス[mol/(m2・s・kPa)]を計算した。さらに、CO2パーミアンスに対するスチームパーミアンスの比(スチームパーミアンス/CO2パーミアンス)を、CO2透過に対するスチーム透過の選択性(スチーム/CO2選択性)として算出した。ガス透過性能の評価条件を下記表に示す。
1.スチーム選択透過膜を含む膜積層体の作製
CsOH、Cs2CO3、CsNO3、CH3COOCs又はCsClをキャリアとして用いて、下記の各表に示す濃度のキャリアと、SSゲルとを含むスチーム選択透過膜を備える膜積層体を、検討1と同様の手順で作製した。各表中、Cs濃度はSSゲル及びキャリア(CsOH)の合計質量(g)に対するCsのモル数の割合であり、キャリア濃度はSSゲル及びキャリアの合計質量に対するキャリアの質量の割合である。
検討1と同様の手順及び条件で、各膜のCO2パーミアンス及びスチーム/CO2選択性を評価した。図4、5、6、7及び8は、それぞれ、CsOH、Cs2CO3、CsNO3、CH3COOCs又はCsClをキャリアとして用いた膜について、スチームパーミアンスと温度との関係、及びスチーム/CO2選択性とCs濃度との関係を示すグラフである。いずれの膜も、高いスチームパーミアンス及びスチーム/CO2選択性を示していることから、各種のCs化合物が、透過性能を向上させるためのキャリアとして有用であることが確認された。Cs濃度がある程度大きくなるとスチーム/CO2選択性が低下する傾向が認められたものの、スチームを選択的に透過し得る程度の選択性は維持された。
1.スチーム選択透過膜を含む膜積層体の作製
KOH、K2CO3、RbOH又はRb2CO3をキャリアとして用いて、下記の各表に示す濃度のキャリアと、SSゲルとを含むスチーム選択透過膜を備える膜積層体を、検討1と同様の手順で作製した。表7~10において、キャリア量はKOH、K2CO3、RbOH又はRb2CO3の量であり、K濃度等はSSゲル及びキャリア(KOH等)の合計質量(g)に対するK等のモル数の割合であり、キャリア濃度はSSゲル及びキャリア(KOH等)の合計質量に対するキャリアの質量の割合である。
検討1と同様の手順及び条件で、各膜のCO2パーミアンス及びスチーム/CO2選択性を評価した。図9、10、11及び12は、それぞれ、KOH、K2CO3、RbOH及びRb2CO3をキャリアとして用いた膜について、スチームパーミアンスと温度との関係、及びスチーム/CO2選択性とCs濃度との関係を示すグラフである。いずれの膜も、高いスチームパーミアンス及びスチーム/CO2選択性を示した。図9~12に示される結果から、K化合物又はRb化合物を用いることにより、SSゲルのみの膜と比較して高温領域でのスチームパーミアンスがさらに向上することが確認された。Rb等の濃度がある程度大きくなるとスチーム/CO2選択性が低下する傾向が認められたものの、スチームを選択的に透過し得る程度の選択性は維持された。
検討1と同様の手順で作製したSSゲルのみの膜について、スイープガスを用いることなく、下記表に示す条件でガス透過性能の評価を行った。
図2に示すガス処理装置と同様の構成を有する装置を準備した。多孔膜4として円筒状のセラミックス多孔膜(アルミナ多孔膜)を用い、その外周面上にSSゲルと、キャリアとしてのCsClとを含む親水性ポリマー層3を担持させた。キャリア濃度は15質量%であった。準備した装置を用いて、下記表に示す条件でガス透過性能の評価を行った。表中のCO2流量、Ar流量は、25℃、1atmの体積流量として示した。H2O供給量は液状のH2Oの供給量として示した。液状のH2Oは加熱により気化され、気化したH2OとCO2との混合ガスをFeed側に供給した。混合ガスのスチーム分率は82%であった。表に示される圧力は絶対圧である。
Claims (9)
- 架橋された親水性ポリマーを含有する、スチーム選択透過膜。
- セシウム化合物、カリウム化合物及びルビジウム化合物からなる群より選ばれる少なくとも1種のアルカリ金属化合物を更に含有する、請求項1に記載のスチーム選択透過膜。
- 親水性ポリマーと、セシウム化合物、カリウム化合物及びルビジウム化合物からなる群より選ばれる少なくとも1種のアルカリ金属化合物と、を含有する、スチーム選択透過膜。
- 前記アルカリ金属化合物がセシウム化合物を含み、前記親水性ポリマー及び前記アルカリ金属化合物の合計質量を基準とするセシウムの濃度が0.003モル/g以下である、請求項2又は3に記載のスチーム選択透過膜。
- 前記アルカリ金属化合物がカリウム化合物及び/又はルビジウム化合物を含み、前記親水性ポリマー及び前記アルカリ金属化合物の合計質量を基準とするカリウム及びルビジウムの合計濃度が0.005モル/g以下である、請求項2又は3に記載のスチーム選択透過膜。
- 請求項1~5のいずれか一項に記載のスチーム選択透過膜に、スチームを含む混合ガス中のスチームを透過させることにより、スチームを前記混合ガスから分離する工程を備える、スチームを混合ガスから分離する方法。
- 当該スチーム選択透過膜の一方の面側にスチームを含む前記混合ガスを供給し、当該スチーム選択透過膜の他方の面側におけるスチームの分圧を前記混合ガスにおけるスチームの分圧よりも低くすることにより、前記スチーム選択透過膜にスチームを透過させる、請求項6に記載の方法。
- 当該スチーム選択透過膜の前記他方の面側におけるスチームの分圧を、スイープガスを実質的に用いることなく前記混合ガスにおけるスチームの分圧よりも低くする、請求項7に記載の方法。
- 前記混合ガスがCO2ガスを含む、請求項6~8のいずれか一項に記載の方法。
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AU2011283590A AU2011283590B2 (en) | 2010-07-26 | 2011-07-26 | Steam permselective membrane, and method using same for separating steam from mixed gas |
JP2012526519A JP6009940B2 (ja) | 2010-07-26 | 2011-07-26 | スチーム選択透過膜、及びこれを用いてスチームを混合ガスから分離する方法 |
RU2013108261/05A RU2579125C2 (ru) | 2010-07-26 | 2011-07-26 | Мембрана с селективной паропроницаемостьюи способ ее использования для отделения пара от газовой смеси |
EP11812489.0A EP2599539B1 (en) | 2010-07-26 | 2011-07-26 | Steam permselective membrane, and method using same for separating steam from mixed gas |
US13/812,042 US9827535B2 (en) | 2010-07-26 | 2011-07-26 | Steam permselective membrane, and method using same for separating steam from mixed gas |
KR1020137004148A KR101780848B1 (ko) | 2010-07-26 | 2011-07-26 | 스팀 선택 투과막, 및 이를 이용하여 스팀을 혼합 가스로부터 분리하는 방법 |
CN201180036285.9A CN103108690B (zh) | 2010-07-26 | 2011-07-26 | 水蒸汽选择透过膜及使用该透过膜从混合气体中分离水蒸汽的方法 |
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US20170232398A1 (en) | 2014-08-11 | 2017-08-17 | Sumitomo Chemical Company, Limited | Composition for co2 gas separation membrane, co2 gas separation membrane and method for producing same, and co2 gas separation membrane module |
JP2018028011A (ja) * | 2016-08-17 | 2018-02-22 | 日本バルカー工業株式会社 | 新規親水性多孔質フッ素樹脂膜の製造方法 |
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Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH01159025A (ja) * | 1987-09-09 | 1989-06-22 | Nederland Centr Org Toegepast Natuur Onder | ガス/水蒸気混合物から水蒸気を除去する方法 |
JPH10113531A (ja) * | 1996-08-14 | 1998-05-06 | Bend Res Inc | 蒸気透過方法 |
JP2004050129A (ja) | 2002-07-23 | 2004-02-19 | Mitsubishi Heavy Ind Ltd | 分離膜エレメント及び分離装置 |
WO2009093666A1 (ja) * | 2008-01-24 | 2009-07-30 | Renaissance Energy Research Corporation | Co2促進輸送膜及びその製造方法 |
JP2010005515A (ja) * | 2008-06-25 | 2010-01-14 | Japan Gore Tex Inc | 複合膜及びそれを用いた水分量調整モジュール |
JP2010082619A (ja) * | 2008-10-02 | 2010-04-15 | Sulzer Chemtech Gmbh | 水分離のための複合膜及びその製造方法 |
Family Cites Families (15)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
GB2072047B (en) * | 1979-08-21 | 1984-03-14 | Lidorenko N S | Gas-permeable membrane method of making it and blood oxygenator based on the use thereof |
US5171449A (en) * | 1992-01-06 | 1992-12-15 | Texaco Inc. | Membrane and method of separation |
US5445669A (en) * | 1993-08-12 | 1995-08-29 | Sumitomo Electric Industries, Ltd. | Membrane for the separation of carbon dioxide |
NL9401233A (nl) * | 1994-03-25 | 1995-11-01 | Tno | Werkwijze voor membraangasabsorptie. |
US6635104B2 (en) * | 2000-11-13 | 2003-10-21 | Mcmaster University | Gas separation device |
US20050211624A1 (en) * | 2004-03-23 | 2005-09-29 | Vane Leland M | Hydrophilic cross-linked polymeric membranes and sorbents |
US7985279B2 (en) * | 2004-05-18 | 2011-07-26 | Asahi Kasei Chemicals Corporation | Gas separator and operating method for the same |
JP2006150323A (ja) * | 2004-11-01 | 2006-06-15 | Japan Gore Tex Inc | 隔膜およびその製法、並びに該隔膜を備えた熱交換器 |
WO2007058698A2 (en) * | 2005-09-13 | 2007-05-24 | Rasirc | Method of producing high purity steam |
JP4965928B2 (ja) * | 2006-08-01 | 2012-07-04 | 株式会社ルネッサンス・エナジー・リサーチ | 二酸化炭素分離装置及び方法 |
JP4965927B2 (ja) | 2006-08-01 | 2012-07-04 | 株式会社ルネッサンス・エナジー・リサーチ | Co2促進輸送膜及びその製造方法 |
JP5443773B2 (ja) * | 2008-01-24 | 2014-03-19 | 株式会社ルネッサンス・エナジー・リサーチ | 二酸化炭素分離装置 |
EP2274079A4 (en) | 2008-03-31 | 2011-08-10 | Commw Scient Ind Res Org | MEMBRANE AND METHOD FOR STEAM DEPOSITION, CLEANING AND RECOVERY |
WO2010117845A2 (en) * | 2009-04-06 | 2010-10-14 | Entegris, Inc. | Non-dewetting porous membranes |
WO2011060088A1 (en) * | 2009-11-10 | 2011-05-19 | Porous Media Corporation | Gel-filled membrane device and method |
-
2011
- 2011-07-26 AU AU2011283590A patent/AU2011283590B2/en active Active
- 2011-07-26 EP EP15192073.3A patent/EP3002053A1/en not_active Withdrawn
- 2011-07-26 WO PCT/JP2011/066983 patent/WO2012014900A1/ja active Application Filing
- 2011-07-26 KR KR1020137004148A patent/KR101780848B1/ko active Search and Examination
- 2011-07-26 US US13/812,042 patent/US9827535B2/en active Active
- 2011-07-26 RU RU2013108261/05A patent/RU2579125C2/ru active
- 2011-07-26 JP JP2012526519A patent/JP6009940B2/ja active Active
- 2011-07-26 CA CA2804302A patent/CA2804302A1/en not_active Abandoned
- 2011-07-26 EP EP11812489.0A patent/EP2599539B1/en active Active
- 2011-07-26 CN CN201180036285.9A patent/CN103108690B/zh active Active
Patent Citations (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH01159025A (ja) * | 1987-09-09 | 1989-06-22 | Nederland Centr Org Toegepast Natuur Onder | ガス/水蒸気混合物から水蒸気を除去する方法 |
JPH10113531A (ja) * | 1996-08-14 | 1998-05-06 | Bend Res Inc | 蒸気透過方法 |
JP2004050129A (ja) | 2002-07-23 | 2004-02-19 | Mitsubishi Heavy Ind Ltd | 分離膜エレメント及び分離装置 |
WO2009093666A1 (ja) * | 2008-01-24 | 2009-07-30 | Renaissance Energy Research Corporation | Co2促進輸送膜及びその製造方法 |
JP2010005515A (ja) * | 2008-06-25 | 2010-01-14 | Japan Gore Tex Inc | 複合膜及びそれを用いた水分量調整モジュール |
JP2010082619A (ja) * | 2008-10-02 | 2010-04-15 | Sulzer Chemtech Gmbh | 水分離のための複合膜及びその製造方法 |
Non-Patent Citations (1)
Title |
---|
See also references of EP2599539A4 |
Cited By (13)
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JP2015127023A (ja) * | 2013-12-27 | 2015-07-09 | 日東電工株式会社 | 透湿性濾材 |
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JP2018043244A (ja) * | 2017-12-22 | 2018-03-22 | 日東電工株式会社 | 透湿性濾材 |
Also Published As
Publication number | Publication date |
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EP2599539A4 (en) | 2014-08-06 |
AU2011283590A1 (en) | 2013-03-07 |
KR101780848B1 (ko) | 2017-10-10 |
US20130199370A1 (en) | 2013-08-08 |
US9827535B2 (en) | 2017-11-28 |
JP6009940B2 (ja) | 2016-10-19 |
CA2804302A1 (en) | 2012-02-02 |
EP2599539A1 (en) | 2013-06-05 |
CN103108690B (zh) | 2017-02-15 |
AU2011283590B2 (en) | 2016-07-21 |
RU2013108261A (ru) | 2014-09-10 |
KR20130137133A (ko) | 2013-12-16 |
CN103108690A (zh) | 2013-05-15 |
EP3002053A1 (en) | 2016-04-06 |
RU2579125C2 (ru) | 2016-03-27 |
JPWO2012014900A1 (ja) | 2013-09-12 |
EP2599539B1 (en) | 2019-09-18 |
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