JP6670583B2 - Bubble liquid concentrator and high-density fine bubble liquid generator - Google Patents

Description

  The present invention relates to a bubble liquid concentrating device for increasing the concentration of bubbles in a supply liquid containing bubbles by a separation membrane, and a high-density fine bubble liquid generating device using the same, and in particular, a diameter of less than 1 μm existing in a liquid. This is useful as a technique for increasing the concentration of bubbles (ultra fine bubbles, UFB).

  2. Description of the Related Art In recent years, technology for producing water containing ultrafine bubbles that is stable for a long time has been actively researched. For example, Non-Patent Document 1 discloses an apparatus that generates a large amount of ultrafine bubbles. Non-Patent Document 2 reports that ultrafine bubbles are stably present in water.

  Also, there are various methods for generating ultrafine bubbles. For example, in the microbubble generating device of Patent Document 1, a mixed fluid in which gas and liquid are mixed is swirled at high speed in a fluid swirling chamber. The bubbles are made finer by the shearing force generated in the swirling flow.

  However, since water containing ultrafine bubbles is generated by mechanically mixing water and air, the amount of fine bubbles generated is about 0.1 billion / mL to about 1 billion / mL. In order to study the use of liquid containing fine bubbles and to improve the efficiency of handling liquid containing fine bubbles, it is important to increase the density of fine bubbles.

  For this reason, Patent Literature 2 discloses that a part of a liquid containing fine bubbles is passed through a filtration filter that does not allow fine bubbles having a diameter of more than 200 nm to easily generate a liquid having a high density of fine bubbles. A high-density microbubble liquid generation method for obtaining a high-density microbubble liquid as the remaining liquid is disclosed. However, Patent Document 2 refers to the pore size of the filtration filter, but does not disclose the material or the like.

Japanese Patent No. 4129290 JP 2014-155920 A

"FZ1N-02 Nanobubble Generator" catalog, [online], May 23, 2011, IDEC Corporation, [searched on December 20, 2011], Internet <URL: http://www.idec.com/ jpja / products / dldata / pdf_b / P1383-0.pdf> Koichi Terasaka and 5 others, "Examination of analysis method of nanobubbles generated by gas-liquid mixed shear method", Proceedings of the Annual Meeting of the Japanese Society of Multiphase Flow 2011, and the Japan Society of Multiphase Flow Annual Meeting 2011 (Kyoto) Committee, August 2011, P424-425

  However, when a filtration filter generally used as a separation membrane is used as in the high-density microbubble liquid generation method of Patent Document 2, bubbles tend to disappear due to contact with the membrane when the bubble liquid is concentrated. It was found that the total amount of air bubbles after concentration was significantly reduced with respect to the total amount of air bubbles in the supplied liquid. For example, as described later, when a UF membrane made of polysulfone, which is widely used as a separation membrane, is used (see Comparative Example 1), even if the stock solution is concentrated 10 times, most of the bubbles disappear, so There is a problem that a bubble-containing liquid having a high concentration cannot be obtained.

  Therefore, an object of the present invention is to provide a bubble liquid concentrating device capable of obtaining a high-concentration bubble-containing liquid, and a high-density fine bubble liquid generating device using the same.

  The present inventors have conducted intensive studies on the material and surface characteristics of the membrane used for concentrating the bubble liquid, and as a result, found that the contact angle between the tangential direction of the bubbles and the surface of the separation membrane in water (hereinafter referred to as the bubble contact angle). It has been found that the above object can be achieved by using a separation membrane having an angle of 140 ° or more, and the present invention has been completed.

That is, the bubble liquid concentration device of the present invention is a bubble liquid concentration device for increasing the concentration of bubbles in a supply liquid containing bubbles by a separation membrane, wherein the separation membrane has at least one surface with air in water. The bubble contact angle is 140 ° or more.

  According to the bubble liquid concentrating device of the present invention, since the bubble contact angle on the surface of the separation membrane used for concentration is 140 ° or more, bubbles are less likely to adhere to the membrane surface. In other words, as shown in FIG. 1, the state of attachment of air bubbles is significantly different between the case of a bubble contact angle of 104 ° in water (FIG. 1a) and the case of a bubble contact angle of 167 ° (FIG. 1c). It is considered that by making it difficult for air bubbles to adhere to the surface, it is possible to transmit liquid while suppressing the disappearance of air bubbles. As a result, it is possible to suppress the disappearance of bubbles due to contact with the membrane during the concentration of the bubble liquid, and it is possible to obtain a high-concentration bubble-containing liquid.

  In particular, in the present invention, it is preferable that the supply liquid contains bubbles having a diameter of less than 1 μm. When the bubble contact angle on the surface of the separation membrane is 140 ° or more, it is possible to make it difficult for the bubbles to adhere to the membrane surface even for fine bubbles having a diameter of less than 1 μm, and it is possible to efficiently separate and concentrate the bubbles. it can.

  In the above, it is preferable that the one surface of the separation membrane has a porous structure having an average pore diameter of 1,000 nm or less or a non-porous structure. With such an average pore size, bubbles having a diameter of less than 1 μm can be efficiently separated and concentrated.

  Further, it is preferable that a hydrophilic polymer porous layer or a non-porous layer is provided on the one surface. By having a hydrophilic polymer porous layer or non-porous layer, a separation membrane having a bubble contact angle in water of 140 ° or more can be easily obtained.

  The bubble liquid concentrating device of the present invention preferably includes a membrane module including a membrane element having the separation membrane, and a container accommodating the membrane element and forming a concentration-side flow path and a permeation-side flow path. As described above, by adopting a structure in which the membrane element is housed in the container, the exchange of the membrane element is facilitated, and the pressure vessel or the like of the conventional membrane separation device can be used.

  It is preferable that the membrane element has a structure in which the supply liquid flows along one membrane surface of the separation membrane and the permeated liquid permeates to the other membrane side of the separation membrane. By adopting such a cross-flow structure, bubbles can be more effectively prevented from adhering to the film surface, and the disappearance of bubbles can be suppressed more reliably.

  Further, it is preferable to provide a circulation flow path for returning the concentrated liquid discharged from the membrane module to the supply liquid. By providing such a circulation channel, it is possible to increase the flow rate of the supply liquid and more effectively prevent bubbles from adhering to the membrane surface.

  On the other hand, a high-density microbubble liquid generator of the present invention includes the bubble liquid concentrator according to any of the above, and a bubble generator that supplies a supply liquid containing bubbles having a diameter of less than 1 μm to the bubble liquid concentrator. It is characterized by the following. According to the high-density microbubble liquid generating device of the present invention, the bubble liquid concentrating device has, on at least one surface, a separation membrane having a bubble contact angle in water of 140 ° or more in water. The bubbles can be prevented from disappearing due to the contact with, and a high-concentration bubble-containing liquid can be obtained.

  Note that the supply liquid generated by the bubble generation device includes not only bubbles having a diameter of less than 1 μm but also bubbles having a diameter of 1 μm to 500 nm. Therefore, bubbles having a diameter of 1 μm or more may be contained in the bubble-containing liquid obtained by the bubble liquid concentrating device of the present invention.

It is a photograph for explaining a bubble contact angle in water, (a) shows a case where the bubble contact angle is 104 °, (b) shows a bubble contact angle of 135 °, and (c) shows a case where the bubble contact angle is 167 °. It is an exploded perspective view showing an example of a membrane element in the present invention. It is a longitudinal section showing an example of a membrane module in the present invention. It is a longitudinal section showing other examples of a membrane module in the present invention. It is a schematic structure figure showing an example of the bubble liquid concentration device of the present invention. It is a schematic structure figure showing other examples of a bubble liquid concentrating device of the present invention. It is a schematic structure figure showing an example of the high-density fine bubble liquid generating device of the present invention. It is a longitudinal section showing an example of a bubble generation device of a high-density fine bubble liquid generation device of the present invention.

  The bubble liquid concentrating device of the present invention is a bubble liquid concentrating device for increasing the concentration of bubbles in a supply liquid containing bubbles by a separation membrane, wherein the separation membrane has a bubble contact angle in water of at least one surface of 140. ° or more. That is, the bubble liquid concentrating device of the present invention includes a separation membrane 2 for bubble liquid concentration, as shown in FIG. 5, for example. The bubble liquid concentrating device of the present invention, as shown in FIG. 3, for example, forms a membrane element 1 having a separation membrane 2 and a concentration-side flow path and a permeation-side flow path by accommodating the membrane element 1. Preferably, a membrane module 30 including the container 31 is provided. First, the bubble liquid concentration separation membrane will be described in detail.

(Separation membrane for bubble liquid concentration)
The separation membrane for bubble liquid concentration in the present invention is used for, for example, concentrating a liquid (bubble liquid) containing bubbles having a diameter of 100 μm or less to increase the concentration of the contained bubbles. It is preferably used when concentrating a liquid containing bubbles of less than 1 μm.

  Bubbles having a diameter of less than 1 μm existing in the liquid are called ultrafine bubbles (UFB), which are stable in the liquid for a long time as compared with the microvalve having a larger diameter, and the liquid has a transparent property.

  In addition, UFB has properties such as gas enrichment, surface activity, crushing, charging, and increase in specific surface area, and can perform single-wafer separation, emulsification, fragrance encapsulation, freshness maintenance, and the like. Therefore, UFB is used not only for semiconductor devices, flat panel displays, electronic devices, solar cells, secondary batteries, etc., but also for foods, beverages, cosmetics, medicines, medical treatment, plant cultivation, new functional materials, removal of radioactive materials, etc. It can be used for various applications.

  The UFB can be generated by various methods. For example, the UFB swirls a mixed fluid in which a gas and a liquid are mixed in a fluid swirling chamber at a high speed, and reduces bubbles by a shear force generated in the swirling flow. Method.

  Examples of the liquid having bubbles include water, an alcohol aqueous solution, ozone water, an acidic aqueous solution, an alkaline aqueous solution, and a surfactant aqueous solution.

  The average diameter of the UFB is usually less than 1 μm, and preferably 0.01 to 0.5 μm, from the viewpoint of exhibiting the above functions. From the viewpoint of increasing the number density after concentration, the number density in the liquid before concentration is preferably at least 0.3 billion / mL or more, more preferably 100 million / mL to 1 billion / mL. preferable.

  The separation membrane for bubble liquid concentration in the present invention is characterized in that at least one surface has a bubble contact angle in water of 140 ° or more, but both surfaces may have a bubble contact angle of 140 ° or more. . When only one surface has a bubble contact angle of 140 ° or more, that surface is disposed on the supply liquid side (a stock solution before concentration) and disposed on the permeate liquid side from the other surface.

  The bubble contact angle in water is 140 ° or more and less than 180 °, but is preferably 145 ° or more, and more preferably 150 °, from the viewpoint of more reliably suppressing the disappearance of bubbles due to contact with the membrane during bubble liquid concentration. The above is more preferable, and 160 or more is most preferable. The bubble contact angle in water is preferably 178 ° or less, more preferably 175 ° or less, and most preferably 170 ° or less from the viewpoint of ease of production of the separation membrane.

  A separation membrane having such a bubble contact angle can be obtained by a method of hydrophilizing at least the surface of a hydrophobic polymer porous layer or by manufacturing a separation membrane with a hydrophilic polymer.

  As in the latter case, when producing a separation membrane with a hydrophilic polymer, for example, a method using a cellulose-based resin, a polyamide-based resin, a polyvinyl alcohol-based resin, or an epoxy resin, or further introducing a crosslinked structure, Can be obtained. Such a separation membrane is preferably one in which a hydrophilic polymer porous layer is formed on one surface of a nonwoven fabric layer from the viewpoints of durability, pressure resistance, permeation flow rate, and the like of the separation membrane. In the present invention, not only flat membranes but also hollow fiber membranes and tubular membranes can be used.

  However, from the viewpoints of durability, manufacturability and the like of the separation membrane, a method of hydrophilizing the surface of the hydrophobic polymer porous layer is preferable. In particular, it is preferable that the hydrophilic treatment is performed by coating with a hydrophilic substance or grafting a hydrophilic polymer.

  Examples of the separation membrane used for the hydrophilization treatment include those having a hydrophobic polymer porous layer. From the viewpoints of durability, pressure resistance, permeation flow rate, etc. of the separation membrane, the polymer porous layer is formed on one side of the nonwoven fabric layer. Are preferably formed. In the present invention, not only flat membranes but also hollow fiber membranes and tubular membranes can be used.

  Examples of the hydrophobic polymer include various polymers such as polysulfone, polyarylethersulfone exemplified by polyethersulfone, polyimide, polyvinylidene fluoride, epoxy resin, polyethylene, polypropylene, and fluororesin. In particular, polysulfone and polyarylethersulfone are preferable because they are chemically, mechanically and thermally stable.

  The separation membrane used for the hydrophilization treatment may be an asymmetric membrane having different average pore sizes on both surfaces of the membrane, or a symmetric membrane, but is preferably an asymmetric membrane from the viewpoint of treatment efficiency during concentration. .

  The average pore size of the separation membrane (the average pore size on the surface with the smaller pore size) is preferably 0.001 to 2 μm, and is preferably 0.05 to 2 μm, from the viewpoint of the pore size after the hydrophilic treatment, the ease of the hydrophilic treatment, and the like. 1 μm is more preferred, and 0.01 to 0.4 μm is even more preferred.

  The thickness of the separation membrane or the polymer porous layer is preferably from 10 to 300 µm, more preferably from 50 to 200 µm. The thickness of the nonwoven fabric layer is preferably from 30 to 200 μm, more preferably from 50 to 150 μm.

The nonwoven fabric layer is not particularly limited as long as it imparts appropriate mechanical strength while maintaining the separation performance and permeation performance of the separation membrane, and a commercially available nonwoven fabric can be used. As this material, for example, a material made of polyolefin, polyester, cellulose or the like is used, and a material obtained by mixing a plurality of materials can also be used. It is particularly preferable to use polyester from the viewpoint of moldability. In addition, a long-fiber nonwoven fabric or a short-fiber nonwoven fabric can be used as appropriate, but a long-fiber nonwoven fabric can be preferably used from the viewpoint of fine fluffing and uniformity of the film surface which cause pinhole defects. In addition, the air permeability of the nonwoven fabric layer alone at this time is not limited to this, but may be about 0.5 to 10 cm ³ / cm ² · s, and 1 to ⁵ cm ³ / Those having a size of about cm ² · s are preferably used.

  Various separation membranes as described above are commercially available, and a separation membrane made of a hydrophilic polymer can be used as it is. In addition, the separation membrane of the hydrophobic polymer can be used for a hydrophilic treatment. Further, the separation membrane can be manufactured by a known method.

  An example of a production method when the polymer of the polymer porous layer is polysulfone will be described. The polymer separation membrane can be produced by a method generally called a wet method or a dry-wet method. First, a solution preparing step in which polysulfone, a solvent and various additives are dissolved, a coating step of coating the nonwoven fabric with the solution, a drying step of evaporating the solvent in the solution to cause microphase separation, a water bath, and the like. Through a fixing step of fixing by dipping in a coagulation bath, a polymer porous layer on the nonwoven fabric can be formed. The thickness of the polymer porous layer can be set by adjusting the solution concentration and the coating amount after calculating the ratio of impregnation into the nonwoven fabric layer.

  Next, the hydrophilic treatment will be described. The hydrophilic treatment is preferably performed by coating with a hydrophilic substance or grafting a hydrophilic polymer.In addition, surface treatment by introducing a hydrophilic group, plasma treatment, excimer laser irradiation, surface treatment by corona discharge treatment, etc. The hydrophilization treatment is also possible by such methods.

  The method of coating a hydrophilic substance includes a method of using a low molecule as a hydrophilic substance and a method of using a polymer, and it is also possible to polymerize using a low molecule to polymerize.

  As a method using a polymer, using a polymer such as polyvinyl alcohol, polyethylene glycol, polyvinylpyrrolidone, polyacrylic acid, hydroxypropylcellulose, and the like, dissolved in a solvent, and then applying or impregnating the solution on a separation membrane, Drying method may be mentioned. At that time, it is also possible to cause a cross-linking reaction between the polymers or the separation membrane using a cross-linking agent or the like.

  Further, even in a method using a low molecular weight as a hydrophilic substance, polyhydric alcohols such as sucrose fatty acid ester, sorbitol and glycerin, surfactants such as sodium dodecylbenzenesulfonate, sodium dodecyl sulfate and sodium lauryl sulfate, sodium lactate Glycerin, or the like, dissolving in a solvent, and applying or impregnating the solution on a separation membrane, followed by drying.

  In addition, it is also possible to use a hydrophilic substance having a functional group reactive with the separation membrane to cause a reaction between the separation membranes.

  When grafting a hydrophilic polymer, for example, a vinyl-type hydrophilic monomer is used. As the vinyl type hydrophilic monomer, acrylic acid, methacrylic acid, hydroxymethyl methacrylic acid, sulfoethyl methacrylic acid, styrene sulfonic acid, or an alkali metal salt thereof can be used.

  When performing grafting, it is preferable to perform electron beam irradiation, chemical graft polymerization using an initiator, photoinitiated graft polymerization, or the like on the separation membrane. Further, after the polymerization is completed, excess monomers are removed.

  As a method of performing coating by performing a polymerization reaction using a low molecule, a method of performing a polymerization reaction using a vinyl-type hydrophilic monomer used for grafting, a polymerization initiator, and a crosslinking agent as necessary, Alternatively, a method using interfacial polymerization as described below can be used.

  In the method using interfacial polymerization, for example, a polyamide-based coating layer is formed, and a homogeneous film having no visible holes is generally obtained. As the polyamide-based coating layer, for example, a polyamide-based separating functional layer obtained by interfacially polymerizing a polyfunctional amine component and a polyfunctional acid halide component on a porous support membrane is well known. It is known that such a polyamide-based separation functional layer has a pleated microstructure, and the thickness of this layer is not particularly limited, but is preferably about 0.05 to 2 μm, and is preferably It is 0.1 to 1 μm. It is known that if this layer is too thin, film surface defects are likely to occur, and if it is too thick, the transmission performance will deteriorate.

  The method for forming the polyamide-based separation functional layer on the surface of the polymer porous layer is not particularly limited, and any known method can be used. For example, a method such as an interfacial polymerization method, a phase separation method, and a thin film coating method can be used. In the present invention, the interfacial polymerization method is particularly preferably used. In the interfacial polymerization method, for example, after coating the polymer porous layer with an aqueous amine solution containing a polyfunctional amine component, interfacial polymerization occurs by bringing an organic solution containing a polyfunctional acid halide component into contact with the amine aqueous solution-coated surface. And a method of forming a skin layer. In this method, after the application of the aqueous amine solution and the organic solution, it is preferable to proceed by removing the excess as appropriate. In this case, the method of removing the film by inclining the target film, the method of blowing off by blowing a gas, the method of rubber And the like, in which a blade is brought into contact with and scraped off is preferably used.

  In the step, the time until the amine aqueous solution and the organic solution come into contact with each other depends on the composition of the amine aqueous solution, the viscosity, and the pore size of the surface of the porous support membrane, and is preferably about 1 to 120 seconds, and is preferably. Is about 2 to 40 seconds. When the interval is too long, the amine aqueous solution permeates and diffuses deep inside the porous support membrane, and a large amount of unreacted polyfunctional amine component remains in the porous support membrane, which may cause a problem. . If the application interval of the solution is too short, an excessive amine aqueous solution remains too much, and the film performance tends to decrease.

  After the contact between the aqueous amine solution and the organic solution, the skin layer is preferably formed by heating and drying at a temperature of 70 ° C. or higher. Thereby, the mechanical strength and heat resistance of the film can be increased. The heating temperature is more preferably from 70 to 200 ° C, particularly preferably from 80 to 130 ° C. The heating time is preferably about 30 seconds to 10 minutes, more preferably about 40 seconds to 7 minutes.

The polyfunctional amine component contained in the amine aqueous solution is a polyfunctional amine having two or more reactive amino groups, and examples thereof include aromatic, aliphatic, and alicyclic polyfunctional amines. Examples of the aromatic polyfunctional amine include m-phenylenediamine, p-phenylenediamine, o-phenylenediamine, 1,3,5-triaminobenzene, 1,2,4-triaminobenzene, 3,5- Examples thereof include diaminobenzoic acid, 2,4-diaminotoluene, 2,6-diaminotoluene, N, N′-dimethyl-m-phenylenediamine, 2,4-diaminoanisole, amidole, xylylenediamine and the like. Examples of the aliphatic polyfunctional amine include ethylenediamine, propylenediamine, tris (2-aminoethyl) amine, and n-phenyl-ethylenediamine. Examples of the alicyclic polyfunctional amine include 1,3-diaminocyclohexane, 1,2-diaminocyclohexane, 1,4-diaminocyclohexane, piperazine, 2,5-dimethylpiperazine, and 4-aminomethylpiperazine. Can be These polyfunctional amines may be used alone or in combination of two or more. In particular, in the present invention, it is preferable to use m-phenylenediamine as a main component from which a highly dense separation function layer can be obtained.
The polyfunctional acid halide component contained in the organic solution is a polyfunctional acid halide having two or more reactive carbonyl groups, and examples thereof include aromatic, aliphatic, and alicyclic polyfunctional acid halides. As the aromatic polyfunctional acid halide, for example, trimesic acid trichloride, terephthalic acid dichloride, isophthalic acid dichloride, biphenyl dicarboxylic acid dichloride, naphthalene dicarboxylic acid dichloride, benzene trisulfonic acid trichloride, benzene disulfonic acid dichloride, chlorosulfonylbenzene And dicarboxylic acid dichloride. Examples of the aliphatic polyfunctional acid halide include, for example, propane dicarboxylic acid dichloride, butane dicarboxylic acid dichloride, pentane dicarboxylic acid dichloride, propane tricarboxylic acid trichloride, butane tricarboxylic acid trichloride, pentane tricarboxylic acid trichloride, glutaryl halide, azide Poil halide and the like. Examples of the alicyclic polyfunctional acid halide include, for example, cyclopropanetricarboxylic acid trichloride, cyclobutanetetracarboxylic acid tetrachloride, cyclopentanetricarboxylic acid trichloride, cyclopentanetetracarboxylic acid tetrachloride, cyclohexanetricarboxylic acid trichloride, tetrahydrochloride Examples thereof include furantetracarboxylic acid tetrachloride, cyclopentanedicarboxylic dichloride, cyclobutanedicarboxylic dichloride, cyclohexanedicarboxylic dichloride, and tetrahydrofurandicarboxylic dichloride. These polyfunctional acid halides may be used alone or in combination of two or more. Above all, it is preferable to use an aromatic polyfunctional acid halide from which a dense separation function layer can be obtained. It is preferable to form a crosslinked structure by using a trifunctional or higher polyfunctional acid halide for at least a part of the polyfunctional acid halide component.

  In the interfacial polymerization method, the concentration of the polyfunctional amine component in the amine aqueous solution is not particularly limited, but is preferably 0.1 to 7% by weight, more preferably 1 to 5% by weight. If the concentration of the polyfunctional amine component is too low, the skin layer tends to have defects, and the salt rejection performance tends to decrease. On the other hand, if the concentration of the polyfunctional amine component is too high, the thickness tends to be too large and the permeation flux tends to decrease.

  The concentration of the polyfunctional acid halide component in the organic solution is not particularly limited, but is preferably 0.01 to 5% by weight, and more preferably 0.05 to 3% by weight. If the concentration of the polyfunctional acid halide component is too low, the unreacted polyfunctional amine component increases, and the skin layer is likely to have defects. On the other hand, if the concentration of the polyfunctional acid halide component is too high, the unreacted polyfunctional acid halide component increases, so that the skin layer becomes too thick and the permeation flux tends to decrease.

  The organic solvent containing the polyfunctional acid halide is not particularly limited as long as it has low solubility in water and does not deteriorate the porous support film, as long as it can dissolve the polyfunctional acid halide component. Examples include saturated hydrocarbons such as heptane, octane, and nonane, and halogen-substituted hydrocarbons such as 1,1,2-trichlorotrifluoroethane. Preferably, it is a saturated hydrocarbon having a boiling point of 300 ° C or lower, more preferably 200 ° C or lower.

An additive for the purpose of improving various performances and handleability may be added to the aqueous amine solution or the organic solution. Examples of the additives include polyvinyl alcohol, polyvinyl pyrrolidone, polymers such as polyacrylic acid, polyhydric alcohols such as sorbitol and glycerin, and surfactants such as sodium dodecylbenzenesulfonate, sodium dodecyl sulfate, and sodium lauryl sulfate. A basic compound such as sodium hydroxide, trisodium phosphate and triethylamine for removing hydrogen halide produced by polymerization, an acylation catalyst, and a solubility parameter of 8 to 14 (cal) described in JP-A-8-224452. / Cm ³ ) ^1/2 compound.

  A coating layer composed of various polymer components may be further provided on the exposed surface of the polyamide-based separation function layer. The polymer component is not particularly limited as long as it does not dissolve the separation function layer and the porous support membrane and does not elute during the water treatment operation.Examples include polyvinyl alcohol, polyvinyl pyrrolidone, hydroxypropyl cellulose, and polyethylene. Glycol and a saponified polyethylene-vinyl acetate copolymer. Among these, it is preferable to use polyvinyl alcohol. In particular, a polyvinyl alcohol having a saponification degree of 99% or more is used, or a polyvinyl alcohol having a saponification degree of 90% or more is crosslinked with the polyamide resin of the skin layer. It is preferable to adopt a configuration that is difficult to elute during water treatment.

  In the present invention, at least one surface of the separation membrane of the hydrophilic polymer or the separation membrane after the hydrophilization treatment has a porous structure with an average pore diameter of 1,000 nm or less, or a non-porous structure, and increases the permeation flow rate to concentrate. From the viewpoint of increasing the processing efficiency of the above, a porous structure having an average pore diameter of 1 to 500 nm is preferable.

(Membrane element)
The membrane element in the present invention is provided with the separation membrane for bubble liquid concentration as described above. The form of such a membrane element is not particularly limited, and examples thereof include a flat membrane type such as a frame and plate type, a spiral type, and a pleated type. When the separation membrane for concentrating bubble liquid is a hollow fiber membrane, a hollow fiber membrane element in which a plurality of hollow fiber membranes are bundled and one or both ends are sealed with a resin or the like is used. Of these membrane elements, spiral membrane elements are generally preferred from the relationship between pressure and flow efficiency.

  As shown in FIG. 2, for example, a spiral-type membrane element includes a laminated body including a separation membrane 2, a supply-side flow path material 6, and a permeation-side flow path material 3, and a perforated central tube around which the laminated body is wound. 5 and a sealing portion 21 for preventing mixing of the supply-side flow path and the permeation-side flow path. In the present embodiment, an example in which a plurality of separation membrane units including the separation membrane 2, the supply-side flow path member 6, and the permeation-side flow path member 3 are wound bodies R wound around the central pipe 5. Is shown.

  The sealing portion 21 for preventing mixing of the supply-side flow path and the permeation-side flow path is formed in an envelope shape by, for example, stacking the separation membrane 2 on both surfaces of the permeation-side flow path material 3 and bonding three sides thereof. When forming the film 4 (bag-like film), the sealing portions 21 are formed on the outer peripheral side edge, the upstream side edge, and the downstream side edge. In addition, it is preferable to provide the sealing portion 21 also between the central pipe 5 and the inner peripheral ends of the upstream side edge and the downstream side edge.

  The envelope-shaped membrane 4 is attached to the central pipe 5 at the opening thereof, and is spirally wound around the outer peripheral surface of the central pipe 5 together with the net-shaped (net-shaped) supply-side flow path material 6 so that the wound body R is formed. It is formed. An upstream end member 10 such as a seal carrier is provided on the upstream side of the wound body R, and a downstream end member 20 such as a telescope prevention member is provided on the downstream side as necessary.

  In such a spiral-type membrane element, normally, the envelope-shaped membrane 4 can wind 20 to 40 sets of the envelope-shaped membranes 4.

  When the above-mentioned membrane element 1 is used, the supply liquid 7 (stock solution before concentration) is supplied from one end face side of the membrane element 1. The supplied supply liquid 7 flows in a direction parallel to the axial direction A1 of the central pipe 5 along the supply-side flow path member 6, and is discharged from the other end face side of the membrane element 1 as a concentrated liquid 9 containing bubbles. Is done. In addition, the permeated liquid 8 that has passed through the separation membrane 2 in the course of the supply liquid 7 flowing along the supply-side flow path member 6 flows from the opening 5a along the permeation-side flow path member 3 as indicated by the dashed arrow in the figure. It flows into the center tube 5 and is discharged from the end of the center tube 5. That is, the membrane element 1 has a structure in which the supply liquid flows along one membrane surface of the separation membrane 2 and the permeated liquid permeates to the other membrane surface of the separation membrane 2.

  In addition, the channel material generally has a role of securing a gap for uniformly supplying a fluid to the membrane surface. As such a channel material, for example, a net, a knitted fabric, a textured sheet, or the like can be used, and a material having a maximum thickness of about 0.1 to 3 mm can be used as needed. In such a flow path material, it is preferable that the pressure loss is low, and it is more preferable that the flow path material generate an appropriate turbulence effect. In addition, the flow path material is installed on both sides of the separation membrane, but it is general to use different flow path materials as the supply side flow path material on the supply liquid side and the permeation side flow path material on the permeate side. . As the supply-side flow path material, a coarse and thick net-like flow path material is used, while as the transmission-side flow path material, a fine-grained woven or knitted flow path material is used.

  The supply-side channel material is provided, for example, on the inner surface side of the two-folded separation membrane. As the structure of the supply-side flow path material, generally, a network structure in which linear objects are arranged in a lattice can be preferably used. The constituent material is not particularly limited, but polyethylene or polypropylene is used. The thickness of the supply-side channel material is generally 0.2 to 2.0 mm, and preferably 0.5 to 1.0 mm.

  The permeate-side channel material is provided, for example, on the outer surface side of the two-folded separation membrane. The permeate-side flow path material is required to support the pressure applied to the membrane from the back side of the membrane and to secure a permeate flow path. Generally, a net or a tricot knit made of polyethylene or polypropylene is used. In particular, a tricot knit made of polyethylene terephthalate is particularly preferably used.

  The center tube is not particularly limited as long as it is a perforated hollow tube having a plurality of small holes on the wall surface of a pipe (hollow tube). When the bubble liquid is concentrated, the permeated liquid that has passed through the separation membrane penetrates into the hollow tube through the hole in the wall surface, and forms a permeate-side flow path. The length of the center tube is generally longer than the length of the element in the axial direction, but a center tube having a connection structure such as dividing into a plurality may be used. The material constituting the central tube is not particularly limited, but a thermosetting resin or a thermoplastic resin is used.

(Membrane module)
The membrane module according to the present invention includes a membrane element including the separation membrane for bubble liquid concentration as described above, and a container that accommodates the membrane element and forms a concentration-side flow path and a permeation-side flow path. is there.

  For example, as shown in FIG. 3, the membrane module 30 shown in the present embodiment includes a spiral-type membrane element 1, a supply unit 32 that accommodates the spiral-type membrane element and supplies a supply liquid 7, and a concentrator that discharges the concentrate 9 A container 31 having a liquid discharge part 33 and a permeate discharge part 34 for discharging the permeate 8 is provided.

  In the illustrated example, the upstream end member 10 holds the sealing material 11, and the sealing material 11 is pressed against the inner wall of the container 31 to guide the supply liquid 7 into the wound body R of the membrane element 1. Has become. The concentrated liquid 9 flowing out from the inside of the wound body R flows through the internal space of the container 31 and the concentrated liquid discharge part 33. Further, one end (the left end in FIG. 3) of the central tube 5 is closed, and the other end (the right end in FIG. 3) is connected to the permeated liquid discharge part 34 of the container 31. When a plurality of the membrane elements 1 are accommodated in the container 31, the central tubes 5 of the adjacent membrane elements 1 are connected via a connecting member (not shown) or the like. With such a structure, the container 31 forms a concentration-side flow path and a permeation-side flow path.

  In the present invention, by supplying a liquid containing bubbles having a diameter of less than 1 μm from the supply unit 32 as the supply liquid 7 in a state where the concentration-side flow path is pressurized, the bubble liquid is separated by the bubble liquid concentration separation membrane. The concentrated concentrate 9 can be discharged from the concentrate discharge part 33. In addition, the permeated liquid 8 that has passed through the separation membrane for bubble liquid concentration can be discharged from the permeated liquid discharge unit 34.

  It is more preferable that the discharged permeate 8 does not contain air bubbles (only the liquid is substantially separated), but the permeate 8 may be separated depending on the properties of the separation membrane, the permeation flow rate, the treatment efficiency of concentration, and the like. May also contain a small amount of air bubbles.

(Bubble liquid concentrator)
The bubble liquid concentrating device of the present invention, as shown in FIG. 5, for example, concentrates bubbles present in a supply liquid by a separation membrane 2, and a supply-side flow path (concentration-side flow path) of a membrane module 30 is provided. In a pressurized state, concentration of the bubble liquid is performed.

  In order to make the concentration-side flow path pressurized, for example, as shown in FIG. The pressure of the concentration-side flow path can be adjusted by adjusting the flow rate by the valve 39 while circulating the concentrate 9 through the pipe 41 through the valve 39 while circulating through the pipe 42. At that time, the pressure and the flow rate can be measured by the pressure gauge 38 and the flow meter 40, respectively. The permeated liquid 8 is discharged to the permeated liquid tank 43.

  The pipe 42 is preferably provided with a valve for adjusting the flow rate in order to facilitate the pressure adjustment.

  When the bubble liquid is concentrated by the bubble liquid concentrating device of the present invention, the pressure of the concentration-side flow path is determined according to the permeation flux of the separation membrane, and may be, for example, 0.05 to 6 MPa. Further, the average linear velocity of the supply liquid on the membrane surface is preferably from 0.1 to 100 cm / sec, more preferably from 1 to 50 cm / sec, from the viewpoint of suppressing disappearance of bubbles. More preferably, it is 5 to 30 cm / sec. If the average linear velocity of the supply liquid is too low, the effect of suppressing the disappearance of bubbles becomes insufficient.

(Other Embodiments of Bubble Liquid Concentrator)
(1) In the above embodiment, an example of a bubble liquid concentrator using a spiral type membrane element having a flat membrane has been described. However, in the present invention, a membrane element having a hollow fiber membrane or a membrane module using the same is used. It is also possible to configure.

  For example, as shown in FIG. 4, a plurality of hollow fiber membranes as the separation membranes 2 are bundled, and one end (the left end in FIG. 4) is sealed so as to be closed by a closing member 15 such as a resin, and the other is sealed. A hollow fiber membrane element whose end (right end in FIG. 4) is sealed with a sealing member 16 made of resin or the like can be used. A sealing material 17 is interposed between the outer periphery of the sealing member 16 and the inner surface of the container 31. As a result, a concentration-side flow path is formed, and by supplying the supply liquid 7 from the supply unit 32, the concentrate 9 in which the bubble liquid is concentrated by the bubble liquid concentration separation membrane is discharged from the concentrate discharge unit 33. Can be. In addition, the permeated liquid 8 that has passed through the separation membrane for bubble liquid concentration can be discharged from the permeated liquid discharge unit 34.

  In the illustrated example, one end (the left end in FIG. 4) is sealed so as to be closed by a closing member 15 such as a resin. It is also possible to use a hollow fiber membrane element whose end is sealed with a sealing member 16 made of resin or the like.

  Further, it is also possible to use a hollow fiber membrane element in which both ends of the hollow fiber membrane are sealed so as to be opened by a sealing member 16 such as a resin. By enclosing the sealing material 17 on the inner surface of the container 31, a concentration-side flow path and a permeation-side flow path can be formed in the container 31. In the membrane module having such a structure, it is possible to supply the liquid for bubble liquid concentration to the inside as well as the outside of the hollow fiber membrane.

  (2) In the above-described embodiment, the example of the bubble liquid concentrating apparatus of the type in which the bubble liquid is concentrated while circulating the liquid is described. However, the bubble liquid concentrating apparatus of the present invention performs the concentration of the bubble liquid in one pass. May be performed.

  For example, as shown in FIG. 6, when the supply liquid 7 is supplied from the supply liquid tank 35 to the container 31 under pressure by the pump 37, while the concentrated liquid 9 is discharged through the pipe 41 through the valve 39, By adjusting the flow rate, the pressure of the concentration-side flow path can be adjusted. Thereby, the permeated liquid 8 can be discharged while the bubble liquid is concentrated.

  (3) In the above-described embodiment, the example of the bubble liquid concentrating device in which the supply liquid having bubbles is stored in the supply liquid tank and then supplied to the membrane module has been described. However, the device which generates the liquid having bubbles having a diameter of less than 1 μm is described. Therefore, it is also possible to directly supply the liquid to the membrane module.

(High-density fine bubble liquid generator)
For example, as shown in FIG. 7, the high-density fine bubble liquid generating apparatus of the present invention supplies the above-described bubble liquid concentrating apparatus of the present invention and the supply liquid containing bubbles having a diameter of less than 1 μm to the bubble liquid concentrating apparatus. And a bubble generating device 50 that performs the operation. In the present invention, the supply liquid may be supplied directly from the bubble generation device 50 to the bubble liquid concentration device, or may be supplied after being stored in the supply liquid tank. As the bubble generation device 50, for example, a device as described in detail in JP-A-2014-155920 can be employed.

  FIG. 8 shows a vertical cross-sectional view of an example of the bubble generation device 50. The bubble generation device 50 mixes a gas and a liquid to generate a liquid containing fine bubbles of the gas. In the present embodiment, water is used as the target liquid 51 before mixing. Air is used as a gas to be mixed with water. The bubble generation device 50 includes a fine bubble generation nozzle 52, a pressurized liquid generation unit 53, a delivery pipe 54a, an auxiliary pipe 54b, a return pipe 54c, a pump 54d, and a liquid storage unit 55. The target liquid 51 is stored in the liquid storage unit 55. By operating the bubble generation device 50, the target liquid 51 becomes the supply liquid.

  The delivery pipe 54a connects the pressurized liquid generation unit 53 and the fine bubble generation nozzle 52. The pressurized liquid generation unit 53 generates a pressurized liquid 56 in which gas is dissolved under pressure, and supplies the generated pressurized liquid 56 to the fine bubble generation nozzle 52 via the delivery pipe 54a. The ejection port of the fine bubble generation nozzle 52 is located in the liquid storage unit 55, and the delivery pipe 54a substantially connects the pressurized liquid generation unit 53 and the liquid storage unit 55.

  By ejecting the pressurized liquid 56 from the fine bubble generation nozzle 52 into the target liquid 51, fine bubbles are generated in the target liquid 51. In the present embodiment, fine air bubbles are generated in the target liquid 51.

  The auxiliary pipe 54b connects the pressurized liquid generation unit 53 and the liquid storage unit 55, similarly to the delivery pipe 54a. The auxiliary pipe 54b guides the liquid discharged together with the excess gas to the liquid storage unit 55 when the excess gas is separated by the pressurized liquid generation unit 53. A pump 54d is provided in the return pipe 54c, and the target liquid 51 is returned from the liquid storage section 55 to the pressurized liquid generation section 53 via the return pipe 54c by the pump 54d.

  The pressurized liquid generation unit 53 includes a mixing nozzle 57 and a pressurized liquid generation container 58. Air flows from the gas inlet of the mixing nozzle 57 via a regulator, a flow meter, or the like. In the mixing nozzle 57, the liquid pumped by the pump 54d and the air are mixed by the mixing nozzle 57 and ejected into the pressurized liquid generation container 58.

  The inside of the pressurized liquid generation container 58 is pressurized by the pressure of the pressurized liquid 56 passing through the fine bubble generation nozzle 52 and the shape of the fine bubble generation nozzle 52 described below, and the pressure is higher than the atmospheric pressure (hereinafter, referred to as “the pressure”). "Pressurized environment"). The fluid (hereinafter, referred to as “mixed fluid 59”) in which the liquid and the gas ejected from the mixing nozzle 57 are mixed with each other while the gas flows through the pressurized liquid generation container 58 under a pressurized environment. Into a pressurized liquid 56 dissolved under pressure.

  The mixing nozzle 57 includes a liquid inlet into which the liquid pumped by the pump 54d flows, a gas inlet into which gas flows, and a mixed fluid outlet from which the mixed fluid 59 is ejected. The mixed fluid 59 is generated by mixing the liquid flowing from the liquid inlet and the gas flowing from the gas inlet. The liquid inlet, the gas inlet, and the mixed fluid jet are each substantially circular. The cross section of the nozzle flow path from the liquid inlet to the mixed fluid ejection port and the cross section of the gas flow path from the gas inlet to the nozzle flow path are also substantially circular. The channel cross section refers to a cross section perpendicular to the central axis of a channel such as a nozzle channel or a gas channel, that is, a cross section perpendicular to the flow of fluid flowing through the channel. In the following description, the area of the cross section of the flow path is referred to as “flow path area”. The nozzle flow path is a Venturi tube in which the flow path area becomes smaller in the middle of the flow path.

  The mixing nozzle 57 includes an introduction portion, a first taper portion, a throat portion, a gas mixing portion, a second taper portion, and an outlet portion, which are sequentially and sequentially arranged from the liquid inlet to the mixed fluid outlet. And The mixing nozzle 57 further includes a gas supply unit having a gas flow path provided therein.

  In the mixing nozzle 57, the liquid flowing from the liquid inlet into the nozzle flow path is accelerated in the throat and the static pressure is reduced. In the throat and the gas mixing section, the pressure in the nozzle flow path is lower than the atmospheric pressure. Become. As a result, the gas is sucked from the gas inlet, passes through the gas flow path, flows into the gas mixing section, is mixed with the liquid, and the mixed fluid 59 is generated. The mixed fluid 59 is decelerated at the second taper portion and the outlet portion to increase the static pressure, and is ejected into the pressurized liquid generating container 58 via the mixed fluid ejection port.

  As shown in FIG. 8, the pressurized liquid generation container 58 includes a first flow path 58a, a second flow path 58b, a third flow path 58c, a fourth flow path 58d, And five flow paths 58e. The flow paths 58a to 58e are pipes extending in the horizontal direction, and the cross section perpendicular to the longitudinal direction of the flow paths 58a to 58e is substantially rectangular. In the present embodiment, the width of the flow channels 58a to 58e is about 40 mm.

  A mixing nozzle 57 is attached to the upstream end (that is, the left end in FIG. 8) of the first flow path 58a, and the mixed fluid 59 ejected from the mixing nozzle 57 is added to the mixing nozzle 57. Under the pressure environment, it flows toward the right side in FIG. In the present embodiment, the mixed fluid 59 is ejected from the mixing nozzle 57 above the liquid level of the mixed fluid 59 in the first flow path 58a, and the mixed fluid 59 immediately after the ejection is mixed with the mixed fluid 59 in the first flow path 58a. It collides directly with the liquid surface before colliding with the downstream wall surface (that is, the right wall surface in FIG. 8). In order to cause the mixed fluid 59 ejected from the mixing nozzle 57 to directly collide with the liquid surface, the length of the first flow path 58a is set to the center of the mixed fluid ejection port 57b of the mixing nozzle 57 and the lower surface of the first flow path 58a. Is preferably larger than 7.5 times the vertical distance between.

  In the pressurized liquid generation unit 53, a part or the whole of the mixed fluid outlet 57b of the mixing nozzle 57 may be located below the liquid level of the mixed fluid 59 in the first flow path 58a. Thus, similarly to the above, in the first flow path 58a, the mixed fluid 59 immediately after being ejected from the mixing nozzle 57 directly collides with the mixed fluid 59 flowing in the first flow path 58a.

  A substantially circular opening 58o is provided on the lower surface of the downstream end of the first flow path 58a, and the mixed fluid 59 flowing through the first flow path 58a flows to the second flow path 58b located below. It falls through the opening 58o. In this way, it falls to the first flow path 58a, the second flow path 58b, the third flow path 58c, and the fourth flow path 58d. In the first flow path 58a to the fourth flow path 58d, the mixed fluid 59 is divided into a liquid layer including bubbles and a gas layer located above the liquid layer.

  In the fourth flow path 58d, it flows (ie, falls) into the fifth flow path 58e located below via a substantially circular opening 58o provided on the lower surface of the downstream end. In the fifth flow path 58e, unlike the first flow path 58a to the fourth flow path 58d, there is no gas layer, and in the liquid filling the fifth flow path 58e, the fifth flow path 58e Is slightly present in the vicinity of the upper surface.

  In the pressurized liquid generation unit 53, the liquid flows down the flow paths 58a to 58e of the pressurized liquid generation container 58 from top to bottom while repeating stepwise graduation (that is, the flow in the horizontal direction and the flow in the downward direction). In the mixed fluid 59 (which alternately flows), the gas gradually dissolves under pressure into the liquid. In the fifth flow path 58e, the concentration of the gas dissolved in the liquid is substantially equal to 60% to 90% of the (saturated) solubility of the gas in a pressurized environment. The surplus gas that has not been dissolved in the liquid exists in the fifth flow path 58e as air bubbles of a size that can be visually recognized.

  The pressurized liquid generation container 58 further includes a surplus gas separation portion 58f extending upward from the upper surface on the downstream side of the fifth flow path 58e, and the surplus gas separation portion 58f is filled with the mixed fluid 59. The cross section perpendicular to the up-down direction of the surplus gas separation unit 58f is substantially rectangular, and the upper end of the surplus gas separation unit 58f is connected to the auxiliary pipe 54b via a pressure-regulating throttle 58g. Bubbles of the mixed fluid 59 flowing through the fifth flow path 58e rise in the surplus gas separating portion 58f and flow into the auxiliary pipe 54b together with a part of the mixed fluid 59.

  In this manner, the surplus gas of the mixed fluid 59 is separated together with a part of the mixed fluid 59, so that the pressurized liquid 56 substantially free of bubbles of at least easily visible size is generated. It is delivered to the delivery pipe 54a connected to the downstream end of the five flow paths 58e. In the present embodiment, gas having a solubility of about twice or more (saturated) solubility of the gas under the atmospheric pressure is dissolved in the pressurized liquid 56. The liquid of the mixed fluid 59 flowing through the flow paths 58a to 58e in the pressurized liquid generation container 58 can be regarded as the pressurized liquid 56 in the course of generation. The mixed fluid 59 flowing into the auxiliary pipe 54b is guided to the target liquid 51 in the liquid storage 55. The auxiliary pipe 54b functions as an auxiliary flow path for preventing the target liquid 51 from decreasing when the pump 54d is operated for a long time.

  An exhaust valve 61 is also provided above the first flow path 58a. The exhaust valve 61 is opened when the pump 54d is stopped, and prevents the mixed fluid 59 from flowing back to the mixing nozzle 57.

  The microbubble generating nozzle 52 includes an introduction portion, a taper portion, and a throat portion that are sequentially arranged from the pressurized liquid inflow port to the pressurized liquid jet port. In the introduction section, the flow channel area is substantially constant at each position in the central axis direction of the nozzle flow channel 0. In the tapered portion, the flow path area gradually decreases in the direction in which the pressurized liquid 56 flows (ie, toward the downstream side). The inner surface of the tapered portion is a part of a substantially conical surface centered on the central axis of the nozzle flow path. In the section including the central axis, the angle formed by the inner surface of the tapered portion is preferably 10 ° or more and 90 ° or less.

  The throat portion 25 connects the tapered portion 24 and the pressurized liquid jet 22. The inner surface of the throat 25 is a substantially cylindrical surface, and the flow passage area in the throat 25 is substantially constant. The diameter of the cross section of the throat 25 is the smallest in the nozzle flow path 20, and the area of the throat 25 is the smallest in the nozzle flow path 20. Although the pressurized liquid 56 passes through the throat 25, the inside of the pressurized liquid generation unit 53 is in a pressurized environment. The gas dissolved in the pressurized liquid 56 is generated as air bubbles, and the air bubbles are miniaturized by the shearing force at the time of pressure reduction.

  The structure of the bubble generation device 50 may be variously changed, and further, a different structure may be used. For example, the fine bubble generation nozzle 52 may include a plurality of pressurized liquid ejection ports. A pressure adjusting valve may be provided between the microbubble generating nozzle 52 and the pressurized liquid generating unit 53, and the pressure applied to the microbubble generating nozzle 52 may be kept constant with high accuracy. The cross-sectional shape of the flow path of the pressurized liquid generation container 58 may be circular. Other means such as mechanical stirring may be used for mixing the gas and the liquid.

  (4) In the above-described embodiment, an example of the bubble liquid concentrating device in which the liquid is circulated when the bubble liquid is concentrated has been described. However, the present invention is not limited to this. Alternatively, a high-density microbubble liquid generation apparatus of a system that repeatedly generates and concentrates a bubble liquid may be used.

For example, the pipe 41 in FIG. 7 is connected to the return pipe 54c of the bubble generation device 50 in FIG.
The concentrated liquid 9 may be supplied to the mixing nozzle 57 again.
Further, the pipe 41 may be circulated to the liquid storage section 55 of the bubble generation device 50. In this case, utilizing the fact that the pressure on the concentration side flow path which was in the pressurized state is reduced, a fine bubble generation nozzle (not shown) is provided on the liquid storage section 55 side of the pipe 41 to reduce the pressure. May be further refined by a shearing force, and a fine bubble generation nozzle may be arranged instead of the valve 39 that pressurizes the concentration-side flow path.

  Hereinafter, the present invention will be described in detail with reference to Examples and Comparative Examples, but the present invention is not limited to these Examples.

(Example of producing separation membrane)
Mixing 18.3% by weight of polysulfone (P-3500, manufactured by Solvay Advanced Polymers) and 81.7% by weight of dimethylformamide on a polyester nonwoven fabric (70 g / m ² , thickness 90 μm, manufactured by Awa Paper Co., Ltd.) The liquid was applied. Thereafter, the polyester nonwoven fabric to which the mixed solution was applied was immersed in pure water at 20 ° C, and further immersed in pure water at 45 ° C. Thus, a polysulfone porous membrane having a thickness of about 130 μm was obtained.

  The separation membrane here was an asymmetric membrane having different average pore diameters on both sides of the membrane, and the average pore diameter on the surface with the smaller pore diameter was 20 nm. In addition, the average pore diameter was measured by reading from SEM surface observation (hereinafter the same).

<Example 1>
The porous membrane made of polysulfone obtained in the production example of the separation membrane was immersed in an aqueous methacrylic acid solution (concentration: 80 wt%) and then taken out. The substrate was irradiated with an electron beam at room temperature to graft-polymerize methacrylic acid onto the substrate. Next, in order to remove the unreacted methacrylic acid monomer and polymer from the base material, the substrate was immersed and washed in hot water at 60 ° C. for 2 hours, and dried in a dryer at 40 ° C. for 2 hours. A separation membrane for use (shown as "graft membrane" in Table 1 described later) was obtained. The average pore size of the surface of the separation membrane having the smaller pore size was 20 nm.

<Example 2>
An aqueous solution (A) was prepared by mixing 3.0 g of m-phenylenediamine, 0.15 g of sodium lauryl sulfate, 6.0 g of benzenesulfonic acid, 3.0 g of triethylamine, and 87.85 g of water. The aqueous solution (A) was applied on the polysulfone porous membrane obtained in the preparation example of the separation membrane to remove excess amine aqueous solution. Next, an isooctane solution containing 0.2% by weight of trimesic acid chloride was further applied. After that, an excess isooctane solution was removed and kept in a dryer at 100 ° C. for 2 minutes to form a skin layer (thickness: about 200 nm, non-porous structure) made of polyamide on the separation membrane. The separation membrane for bubble liquid concentration of Example 2 (shown as “coating membrane” in Table 1 described later) was obtained.

<Comparative Example 1>
The polysulfone porous membrane obtained in the production example of the separation membrane was used as a separation membrane for bubble liquid concentration (indicated as “polysulfone membrane” in Table 1 described later) without surface treatment.

(Measurement of bubble contact angle in water)
After immersing the prepared separation membranes for foam liquid concentration of Examples 1 and 2 and Comparative Example 1 in pure water at 25 ° C. for 10 minutes, an automatic contact angle measuring device (trade name “DM-300” manufactured by Kyowa Interface Science Co., Ltd.) )), The contact angle of air (bubbles) adhering to the separation membrane for bubble liquid concentration was measured. The measurement was performed on N-cells having a bubble diameter of 400 to 500 μm, N = 5 times. At this time, the measurement was performed while supplying air bubbles with a syringe needle.

(Measurement of UFB number density before and after concentration)
The bubble liquid was concentrated using the bubble liquid concentration shown in FIG. 5, and the number density of the ultrafine bubbles was measured.

  That is, the prepared flat membrane-shaped separation membranes for bubble liquid concentration of Examples 1 and 2 and Comparative Example 1 were cut into a predetermined shape and size, and a cell for flat membrane evaluation (C10-T, manufactured by Nitto Denko Corporation). ). Next, 4 L of ultra-fine bubble water (mode diameter of bubbles is 0.1 μm, number density of 100 million / mL) generated by an ultra-fine bubble generator (FZ1N-02, manufactured by IDEC) is contained. An ultra-fine bubble raw water was supplied at a pressure of 0.5 MPa and a flow rate of 1 L / min to the side having a smaller pore diameter (separation surface side) of the bubble liquid concentrating separation membrane. By this operation, filtration was performed while circulating the ultrafine bubble raw water until the raw water tank reached 0.4 L to obtain a 10-fold concentrated liquid.

  The number density of the ultrafine bubble raw water and the number density of the ultrafine bubbles contained in the 10-fold concentrated solution were respectively measured by a nanoparticle analyzer (NS500, manufactured by Nanosight Corporation), and the increase rate of the number density of the ultrafine bubbles was calculated.

Table 1 shows the measurement results of the above measurements of the separation membranes for foam liquid concentration according to Examples 1 and 2 and Comparative Example 1.

  As shown in the results of Table 1, as in Examples 1 and 2, when a separation membrane having a bubble contact angle in water of 140 ° or more was used by surface treatment, the membrane and the membrane were concentrated during bubble liquid concentration. This suppresses the disappearance of bubbles due to contact with the liquid, thereby obtaining a high-concentration bubble-containing liquid. In contrast, when a polysulfone separation membrane, which is widely used as a separation membrane, is used, even if the stock solution is concentrated 10 times, most of the bubbles disappear, so that a high-concentration bubble-containing liquid can be obtained. Could not.

<Example 3>
In Example 1, the surface treatment (coating) of polyvinyl alcohol (manufactured by Kuraray Co., Ltd., product name: KM-118) was performed using the polysulfone porous membrane (ungrafted product) obtained in the production example of the separation membrane. Except for the above, a separation membrane for foam liquid concentration (bubble contact angle of 155 °) was prepared in exactly the same manner as in Example 1, and the UFB number density before and after concentration was measured. As a result, the increase rate of the UFB number density at the time of 10-fold concentration was 3.7 times. The coating with polyvinyl alcohol was performed as follows.

  The polysulfone porous membrane (ungrafted) obtained in the production example of the separation membrane was immersed in a 10% by weight aqueous solution of isopropyl alcohol to make it wet, and then 0.05% by weight of polyvinyl alcohol was applied to the polysulfone membrane side. The aqueous solution was applied and dried in an oven at 80 ° C.

<Comparative Examples 2 to 4>
Separation membrane made of hydrophobic polyethersulfone (average pore diameter 10 nm, contact angle 75 °), separation membrane made of polyvinylidene fluoride (average pore diameter 500 nm, contact angle 56 °), separation membrane made of epoxy resin (average pore diameter 50 nm, contact angle 110) °) was used as a separation membrane for foam liquid concentration without any surface treatment.

  As a result of measuring the UFB number density before and after concentration, the rate of increase of the UFB number density at the time of 10- to 50-fold concentration was less than 2 times.

DESCRIPTION OF SYMBOLS 1 Membrane element 2 Separation membrane 3 Permeation side flow path material 4 Envelope membrane 5 Central pipe 6 Supply side flow path material 7 Supply liquid 8 Permeate 9 Concentrate 30 Membrane module 31 Container 50 Bubble generator

Claims (8)

In a bubble liquid concentrator for increasing the concentration of bubbles in the supply liquid containing bubbles by a separation membrane,
The bubble liquid concentrating device according to claim 2, wherein at least one surface of the separation membrane has a bubble contact angle with air in water of 140 ° or more.   The bubble liquid concentrating device according to claim 1, wherein the supply liquid contains bubbles having a diameter of less than 1 µm.   The bubble liquid concentrating device according to claim 1 or 2, wherein the one surface of the separation membrane has a porous structure having an average pore diameter of 1,000 nm or less or a non-porous structure.   The bubble liquid concentrator according to any one of claims 1 to 3, wherein the separation membrane has a polymer porous layer or a non-porous layer having hydrophilicity on the one surface.   The bubble liquid concentration according to any one of claims 1 to 4, further comprising a membrane module including a membrane element having the separation membrane, and a container accommodating the membrane element and forming a concentration-side flow path and a permeation-side flow path. apparatus.   The bubble liquid according to claim 5, wherein the membrane element has a structure in which the permeate is allowed to permeate to the other membrane surface side of the separation membrane while the supply liquid flows along one membrane surface of the separation membrane. Concentrator.   The bubble liquid concentrating device according to claim 5 or 6, further comprising a circulation flow path for returning the concentrated liquid discharged from the membrane module to the supply liquid. A high-density microbubble liquid generation device, comprising: the bubble liquid concentration device according to any one of claims 1 to 7; and a bubble generation device that supplies a supply liquid containing bubbles having a diameter of less than 1 µm to the bubble liquid concentration device.