JP2012061455A - Platinum group metal-supported catalyst, method for producing the same, method for producing hydrogen peroxide-decomposed water, and method for producing dissolved oxygen-removed water - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a high-performance catalyst capable of decomposing/removing hydrogen peroxide or removing dissolved oxygen even when water passing is performed at SV (space velocity) exceeding 2,000 hand even when the height of the layer packed with the high-performance catalyst is thinned.SOLUTION: A platinum group metal-supported catalyst is obtained by supporting platinum group metal particles each having 1-100 nm average particle size on a monolithic organic porous body. The uniformity degree of the platinum group metal particles is ≤10 and the supported amount of the platinum group metal particles is 0.004-20 wt.% in a dried state thereof.

Description

  The present invention relates to a platinum group metal-supported catalyst for removing oxidizing substances such as hydrogen peroxide and dissolved oxygen in ultrapure water, which are used in water for precision processing such as power plant water and semiconductor manufacturing. It is.

  It is known that dissolved oxygen in the water used at power plants will cause corrosion of components such as pipes and heat exchangers. In particular, dissolved oxygen is used as much as possible in the primary and secondary systems of nuclear power plants. There is a need to reduce.

  In the semiconductor manufacturing industry, silicon wafers are cleaned using ultrapure water from which impurities are highly removed. Ultrapure water generally removes part of suspended matter and organic matter contained in raw water (river water, groundwater, industrial water, etc.) in the pretreatment process, and then treats the treated water with the primary pure water system and secondary pure water. Manufactured by sequential processing in an aqueous system (subsystem) and supplied to a use point for wafer cleaning. Such ultrapure water has such a purity that it is difficult to quantify the impurities, but it does not have no impurities at all.

  For example, dissolved oxygen contained in ultrapure water forms a natural oxide film on the surface of a silicon wafer. When a natural oxide film is formed on the wafer surface, it prevents growth of epitaxial Si thin films at low temperatures, hinders precise control of gate oxide film pressure and film quality, and causes increase in contact resistance of contact holes. It becomes. Therefore, it is necessary to suppress the formation of the natural oxide film on the wafer surface as much as possible.

  Therefore, in the ultrapure water production apparatus, particularly in the primary pure water system, dissolved oxygen is reduced by using a deaeration device. With this deaeration device, the dissolved oxygen concentration in the water to be treated (primary pure water) at the entrance of the secondary pure water system is usually reduced to 100 μg / L or less. Furthermore, it may be controlled to 10 μg / L or less.

  In the above-described production of ultrapure water, organic substances are generally decomposed by an ultraviolet oxidizer installed in a secondary pure water system. Since hydrogen peroxide is by-produced in the process of ultraviolet oxidation, it is common that hydrogen peroxide remains in the treated water of the ultraviolet oxidation apparatus. This hydrogen peroxide is partially decomposed in the polisher process of the secondary pure water system to generate oxygen, and increase the dissolved oxygen concentration in the treated water.

  Therefore, a method has been proposed in which hydrogen peroxide contained in the treated water of the ultraviolet oxidation apparatus is adsorbed and removed using a synthetic carbon-based granular adsorbent (Japanese Patent Laid-Open No. 9-29233). According to this method, it is possible to suppress the formation of a natural oxide film on the wafer surface because hydrogen peroxide itself remaining in the treated water of the ultraviolet oxidation apparatus is removed. However, this method requires a large adsorption tower filled with a large amount of a synthetic carbon-based particulate adsorbent in order to achieve a predetermined hydrogen peroxide removal rate.

  In addition, a method has been proposed in which hydrogen peroxide contained in treated water of an ultraviolet oxidation apparatus is decomposed with a catalyst in which platinum group metal nanocolloid particles are supported on a carrier (Japanese Patent Laid-Open No. 2007-185587).

JP-A-9-29233 (Claims) JP 2007-185587 A (Claims)

However, the catalysts described in JP-A-2007-185587, can only be used at relatively low region passing water space velocity (SV) is a 100～2000H ^-1, the SV exceeds 2000h ^-1, peroxide There was a disadvantage that the decomposition and removal of hydrogen was insufficient. Also, the packed bed height of the catalyst is required to be about 100 mm, and if the packed bed height is less than 100 mm, the decomposition and removal of hydrogen peroxide may be insufficient even if the SV is 100 to 2000 h ^−1. .

Therefore, the object of the present invention is to allow the decomposition and removal of hydrogen peroxide or the removal of dissolved oxygen even when water is passed through a large SV with an SV exceeding 2000 h ⁻¹ , and the catalyst packed bed height is reduced. It is an object to provide a high-performance catalyst that can decompose hydrogen peroxide or remove dissolved oxygen.

In such a situation, the present inventors have conducted intensive studies, and as a result, a fluid containing platinum group metal particles having an average particle size of 1 to 100 nm and a uniform particle size distribution of a uniform degree of 10 or less, for example, an average A monolithic organic porous material or a monolithic organic porous ion exchanger is brought into contact with a supercritical fluid containing platinum group metal particles having a particle size of 1 to 100 nm and a uniform particle size distribution with a homogeneity of 10 or less. By doing so, a platinum group metal-supported catalyst in which platinum group metal particles having an average particle size of 1 to 100 nm and a uniform degree of 10 or less and a uniform particle size distribution is supported in the pores of the organic porous body is obtained. Such a platinum group metal-supported catalyst is capable of decomposing and removing hydrogen peroxide or removing dissolved oxygen even when water is passed through a large SV with an SV exceeding 2000 h ⁻¹ . It has been found that hydrogen peroxide can be decomposed or dissolved oxygen can be removed even if the packed bed height is reduced, and the present invention has been completed.

  That is, the present invention (1) is a platinum group metal-supported catalyst in which platinum group metal particles having an average particle diameter of 1 to 100 nm are supported on a monolithic organic porous body or a monolithic organic porous ion exchanger. A platinum group metal-supported catalyst, wherein the platinum group metal particles have a degree of homogeneity of 10 or less and the supported amount of the platinum group metal particles is 0.004 to 20% by weight in a dry state. To do.

  Further, the present invention (2) provides a monolithic organic porous material or a monolithic organic porous ion exchanger in a fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less. A platinum group metal supporting step of obtaining a platinum group metal supported catalyst by supporting the platinum group metal particles on the monolithic organic porous material or the monolithic organic porous ion exchanger by contacting A feature of the present invention is to provide a method for producing a platinum group metal supported catalyst.

  In the present invention (3), the platinum group metal supported catalyst of the above (1) is brought into contact with water to be treated containing hydrogen peroxide, so that the hydrogen peroxide in the water to be treated containing hydrogen peroxide The present invention provides a method for producing hydrogen peroxide-decomposed water characterized by being decomposed and removed.

  Further, in the present invention (4), in the presence of the platinum group metal supported catalyst of the above (1), oxygen is produced by reacting dissolved oxygen in hydrogen to be treated containing oxygen with hydrogen to generate water. Disclosed is a method for producing dissolved oxygen-removed treated water, which comprises removing dissolved oxygen from water to be treated.

According to the platinum group metal-supported catalyst of the present invention, hydrogen peroxide can be decomposed or dissolved oxygen can be removed even when the SV is passed through a large SV exceeding 2000 h ^−1. Even if the layer height is reduced, hydrogen peroxide can be decomposed or dissolved oxygen can be removed.

It is a SEM photograph of the example of the form of the 1st monolith. It is a SEM photograph of the example of the form of the 2nd monolith. It is a SEM photograph of the example of the form of the 3rd monolith. It is the figure which transcribe | transferred the frame | skeleton part which appears as a cross section of the SEM photograph of FIG. It is a SEM photograph of the example of the form of the 4th monolith. It is a schematic diagram of the co-continuous structure of a 4th monolith and a monolith ion exchanger. It is a SEM photograph of the example of a form of a monolith intermediate (4). It is typical sectional drawing of a protrusion. It is a SEM photograph of the example of a form of the 5-1 monolith. It is a schematic diagram which shows the basic structure of a 6th monolith and a monolith ion exchanger. It is a SEM photograph of the example of the form of the 6th monolith.

  The platinum group metal-supported catalyst of the present invention is a platinum group metal-supported catalyst in which platinum group metal particles having an average particle diameter of 1 to 100 nm are supported on a monolithic organic porous body or a monolithic organic porous ion exchanger. A platinum group metal-supported catalyst, wherein the platinum group metal particles have a degree of uniformity of 10 or less, and the amount of the platinum group metal particles supported is 0.004 to 20% by weight.

  The monolithic organic porous body is a porous body having a skeleton formed of an organic polymer and a large number of communication holes serving as a flow path of water to be treated between the skeletons. The monolithic organic porous ion exchanger is a porous body in which an ion exchange group is introduced into the monolithic organic porous body. In the present specification, “monolithic organic porous material” is also simply referred to as “monolith”, and “monolithic organic porous ion exchanger” is also simply referred to as “monolith ion exchanger”, The “monolithic organic porous intermediate” that is the body (precursor) is also simply referred to as “monolith intermediate”.

<Monolithic organic porous body and monolithic organic porous ion exchanger>
Examples of the monolith include the first monolith to the sixth monolith shown below. Examples of the monolith ion exchanger include the following first to sixth monolith ion exchangers.

<Description of First Monolith and First Monolith Ion Exchanger>
In the platinum group metal-supported catalyst of the present invention, the first monolith and the first monolith ion exchanger serving as the support for the platinum group metal particles have an average diameter of 1 in a dry state in the walls of the macropores and the macropores connected to each other. It is an organic porous body having an open cell structure having a common opening (mesopore) of ˜1000 μm and a total pore volume of 1 to 50 ml / g in a dry state. The first monolith ion exchanger has ion exchange groups, the ion exchange groups are uniformly distributed, and the ion exchange capacity per weight in a dry state is 0.5 to 5.0 mg equivalent / g. A monolith ion exchanger.

  In the first monolith and the first monolith ion exchanger, bubble-like macropores overlap each other, and the overlapping portion is in a dry state and has an average diameter of 1 to 1000 μm, preferably 10 to 200 μm, particularly preferably 20 to 100 μm. It is a continuous macropore structure that becomes an opening (mesopore), most of which has an open pore structure. In the open pore structure, when water is flowed, the inside of bubbles formed by the macropores and the mesopores becomes a flow path. The number of overlapping macropores is 1 to 12 for one macropore, and 3 to 10 for many. FIG. 1 shows a scanning electron microscope (SEM) photograph of an example of the form of the first monolith. The first monolith shown in FIG. 1 has a large number of bubble-like macropores. The macropores overlap each other, and the overlapping portion is a continuous macropore structure in which a common opening (mesopore) is formed, and most of them have an open pore structure. If the average diameter in the dry state of the mesopores is less than 1 μm, the pressure loss during water passage becomes extremely large, which is not preferable. Alternatively, the contact with the monolith ion exchanger becomes insufficient, and the hydrogen peroxide decomposition characteristic or the dissolved oxygen removal characteristic is deteriorated. Since the structure of the first monolith and the first monolith ion exchanger has the above-mentioned open cell structure, the macropore group and the mesopore group can be formed uniformly, and described in JP-A-8-252579. Compared with such a particle-aggregated porous body, the pore volume and specific surface area can be significantly increased.

  In the present invention, the average diameter of the opening of the first monolith in the dry state and the first monolith ion exchanger is measured by a mercury intrusion method. In addition, the average diameter of the opening of the first monolith or the first monolith ion exchanger in the wet state of water is the average diameter of the opening of the first monolith or the first monolith ion exchanger in the dry state. It is a value calculated by multiplication. Specifically, the diameter of the first monolith (or monolith ion exchanger) in the water wet state is x1 (mm), and the first monolith (or monolith ion exchanger) in the water wet state is dried, The diameter of the obtained first monolith (or monolith ion exchanger) in the dry state is y1 (mm), and the first monolith (or monolith ion exchanger) in the dry state is measured by a mercury intrusion method. Assuming that the average diameter of the opening is z1 (μm), the average diameter (μm) of the opening of the first monolith (or monolith ion exchanger) in the water wet state is calculated by the following equation. It is calculated by “average diameter (μm) = z1 × (x1 / y1) of openings of the first monolith (or monolith ion exchanger) in a water-wet state”. Further, the average diameter of the opening of the first monolith in the dry state before the introduction of the ion exchange group, and the water wet state relative to the first monolith in the dry state when the ion exchange group is introduced into the first monolith in the dry state. When the swelling ratio of the first monolith ion exchanger is known, the average diameter of the opening of the first monolith in the dry state is multiplied by the swelling ratio to obtain the average of the opening of the first monolith ion exchanger in the water wet state. The diameter can also be calculated.

  The total pore volume per weight of the first monolith and the first monolith ion exchanger in the dry state is 1 to 50 ml / g, preferably 2 to 30 ml / g. If the total pore volume is less than 1 ml / g, it is not preferable because the pressure loss at the time of passing water increases, and further, the amount of permeated water per unit cross-sectional area decreases, and the treatment capacity decreases. Absent. On the other hand, if the total pore volume exceeds 50 ml / g, the mechanical strength is lowered, and the monolith and the monolith ion exchanger are greatly deformed particularly when water is passed at a high flow rate. Furthermore, the contact efficiency between the water to be treated, the monolith and the monolith ion exchanger, and the platinum group metal particles supported on the monolith is lowered, and the catalytic effect is also lowered. In the conventional particulate porous ion exchange resin, the total pore volume is 0.1 to 0.9 ml / g at the most. Those having a specific surface area can be used.

  In addition, the pressure loss at the time of making water permeate | transmit the 1st monolith and the 1st monolith ion exchanger is the pressure at the time of water-flowing at the water flow rate (LV) of 1 m / h through the column which filled this with 1 m. In terms of loss (hereinafter referred to as “differential pressure coefficient”), 0.005 to 0.5 MPa / m · LV is preferable, and 0.005 to 0.05 MPa / m · LV is particularly preferable. If the differential pressure coefficient and the total pore volume are in the above ranges, when this is used as a catalyst, the contact area with the water to be treated is large, and the water to be treated can be smoothly circulated. Is demonstrated.

  In the first monolith and the first monolith ion exchanger, the material constituting the skeleton is an organic polymer material having a crosslinked structure. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.3 to 10 mol%, preferably 0.3 to 5 mol% of crosslinked structural units with respect to all structural units constituting the polymer material. It is preferable. If the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, if it exceeds 10 mol%, it may be difficult to introduce an ion exchange group.

  There is no restriction | limiting in particular in the kind of organic polymer material which comprises frame | skeleton of 1st monolith and 1st monolith ion exchanger, For example, polystyrene, poly (alpha-methyl styrene), polyvinyl toluene, polyvinyl benzyl chloride, polyvinyl biphenyl, Aromatic vinyl polymers such as polyvinyl naphthalene; polyolefins such as polyethylene and polypropylene; poly (halogenated polyolefins) such as polyvinyl chloride and polytetrafluoroethylene; nitrile polymers such as polyacrylonitrile; polymethyl methacrylate and polyglycidyl methacrylate And cross-linked polymers such as (meth) acrylic polymers such as polyethyl acrylate. The organic polymer may be a polymer obtained by copolymerizing a single vinyl monomer and a crosslinking agent, a polymer obtained by polymerizing a plurality of vinyl monomers and a crosslinking agent, or two or more kinds of polymers. It may be blended. Among these organic polymer materials, the cross-linking weight of the aromatic vinyl polymer is determined by the ease of forming a continuous macropore structure, the ease of introduction of ion exchange groups and the high mechanical strength, and the high stability to acids or alkalis. A styrene-divinylbenzene copolymer and a vinylbenzyl chloride-divinylbenzene copolymer are particularly preferable materials.

  The ion exchange group introduced into the first monolith ion exchanger is the same in the second monolith ion exchanger to the sixth ion exchanger, and is a cation exchange group or an anion exchange group. Examples of the cation exchange group include a carboxylic acid group, an iminodiacetic acid group, a sulfonic acid group, a phosphoric acid group, and a phosphoric ester group. Examples of anion exchange groups include trimethylammonium group, triethylammonium group, tributylammonium group, dimethylhydroxyethylammonium group, dimethylhydroxypropylammonium group, methyldihydroxyethylammonium group, quaternary ammonium group, tertiary sulfonium group, phosphonium group. Etc.

  In the first monolith ion exchanger (the same applies to the second monolith ion exchanger to the sixth ion exchanger), the introduced ion exchange group is not only the surface of the porous body but also the porous body. Evenly distributed even inside the skeleton. Here, “ion exchange groups are uniformly distributed” means that the distribution of ion exchange groups is uniformly distributed on the surface and inside the skeleton in the order of at least μm. This is the distribution of ion exchange groups. In the case of anion exchange groups, the counter anion is ion exchanged with chloride ions, bromide ions, etc., and then confirmed by using EPMA (Electron Probe Micro Analyzer). In the case of a cation exchange group, for example, in the case of a sulfonic acid group, the sulfonic acid group can be confirmed by mapping a sulfur atom using EPMA. In addition, if the ion exchange groups are uniformly distributed not only on the surface of the monolith but also within the skeleton of the porous body, the physical and chemical properties of the surface and the interior can be made uniform, so that the swelling and shrinkage can be achieved. The durability against is improved.

  The ion exchange capacity per weight of the first monolith ion exchanger in the dry state is 0.5 to 5.0 mg equivalent / g. If the ion exchange capacity per weight in the dry state is in the above range, in the case of a monolith ion exchanger having an OH-type anion exchange group, the basicity in the vicinity of the catalyst support increases, and the hydrogen peroxide decomposition characteristics or Increases dissolved oxygen removal properties. In addition, when the ion exchange capacity per weight in a dry state exceeds 5.0 mg equivalent / g, the volume change of swelling and shrinkage of the monolith ion exchanger due to the change of the ion form tends to be too large. The ion exchange capacity per volume of the first monolith ion exchanger in the wet state is not particularly limited, but is usually 0.05 to 0.5 mg equivalent / ml. Note that the ion exchange capacity of the porous body in which the ion exchange group is introduced only on the surface cannot be determined unconditionally depending on the kind of the porous body or the ion exchange group, but is at most 500 μg equivalent / g.

<Method for producing first monolith and first monolith ion exchanger>
Although it does not restrict | limit especially as a manufacturing method of a 1st monolith, An example of the manufacturing method according to the method of Unexamined-Japanese-Patent No. 2002-306976 is shown below. That is, the first monolith is prepared by mixing an oil-soluble monomer not containing an ion exchange group, a surfactant, water and a polymerization initiator as necessary to obtain a water-in-oil emulsion and polymerizing the emulsion. Is obtained. Such a manufacturing method of the first monolith is preferable in that the porous structure of the monolith can be easily controlled.

  The oil-soluble monomer that does not contain an ion exchange group used in the production of the first monolith contains neither a cation exchange group such as a carboxylic acid group or a sulfonic acid group nor an anion exchange group such as a quaternary ammonium group, This refers to a lipophilic monomer that has a low solubility in water. Specific examples of these monomers include styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, divinyl benzene, ethylene, propylene, isobutene, butadiene, isoprene, chloroprene, vinyl chloride, vinyl bromide, vinylidene chloride, tetrafluoroethylene. , Acrylonitrile, methacrylonitrile, vinyl acetate, methyl acrylate, ethyl acrylate, butyl acrylate, 2-ethylhexyl acrylate, trimethylolpropane triacrylate, butanediol diacrylate, methyl methacrylate, ethyl methacrylate, propyl methacrylate , Butyl methacrylate, 2-ethylhexyl methacrylate, cyclohexyl methacrylate, benzyl methacrylate, glycidyl methacrylate, ethylene glycol dimethyl ester Acrylate, and the like. These monomers can be used singly or in combination of two or more. However, in the present invention, a crosslinkable monomer such as divinylbenzene or ethylene glycol dimethacrylate is selected as at least one component of the oil-soluble monomer, and its content is preferably 0.3 to 10 mol% in the total oil-soluble monomer. Is preferably 0.3 to 5 mol% from the viewpoint of quantitatively introducing ion-exchange groups in a later step and securing a practically sufficient mechanical strength.

  The surfactant used in the production of the first monolith is not particularly limited as long as it can form a water-in-oil (W / O) emulsion when an oil-soluble monomer containing no ion exchange group and water are mixed. There is no limitation, such as sorbitan monooleate, sorbitan monolaurate, sorbitan monopalmitate, sorbitan monostearate, sorbitan trioleate, polyoxyethylene nonylphenyl ether, polyoxyethylene stearyl ether, polyoxyethylene sorbitan monooleate Nonionic surfactants; Anionic surfactants such as potassium oleate, sodium dodecylbenzenesulfonate, dioctyl sodium sulfosuccinate; cationic surfactants such as distearyldimethylammonium chloride; lauryldimethylbetaine, etc. It can be used sex surfactant. These surfactants can be used singly or in combination of two or more. The water-in-oil emulsion refers to an emulsion in which an oil phase is a continuous phase and water droplets are dispersed therein. The amount of the surfactant added may vary depending on the type of oil-soluble monomer and the size of the target emulsion particles (macropores), but it cannot be generally stated, but the total amount of oil-soluble monomer and surfactant Can be selected within a range of about 2 to 70%. Moreover, although not necessarily essential, in order to control the bubble shape and size of the monolith, alcohols such as methanol and stearyl alcohol; carboxylic acids such as stearic acid; hydrocarbons such as octane, dodecane and toluene; tetrahydrofuran, dioxane and the like Cyclic ether can coexist in the system.

  In the production of the first monolith, when forming the monolith by polymerization, a compound that generates radicals by heat and light irradiation is suitably used as the polymerization initiator used as necessary. The polymerization initiator may be water-soluble or oil-soluble. For example, azobisisobutyronitrile, azobisdimethylvaleronitrile, azobiscyclohexanenitrile, azobiscyclohexanecarbonitrile, benzoyl peroxide, persulfate Examples include potassium, ammonium persulfate, hydrogen peroxide-ferrous chloride, sodium persulfate-sodium acid sulfite, and tetramethylthiuram disulfide. However, in some cases, there is a system in which the polymerization proceeds only by heating or light irradiation without adding a polymerization initiator, and in such a system, the addition of the polymerization initiator is unnecessary.

  In the production of the first monolith, the mixing method for mixing the oil-soluble monomer not containing an ion exchange group, a surfactant, water and a polymerization initiator to form a water-in-oil emulsion is not particularly limited. Without mixing each component at once, oil-soluble monomer, surfactant and oil-soluble polymerization initiator oil-soluble component and water or water-soluble polymerization initiator water-soluble component separately After uniformly dissolving, a method of mixing each component can be used. There is no particular limitation on the mixing apparatus for forming the emulsion, and ordinary mixers, homogenizers, high-pressure homogenizers, and objects to be treated are placed in a mixing container, and the mixing container is tilted and revolved around the revolution axis. While rotating, a so-called planetary stirring device that stirs and mixes the object to be processed can be used, and an appropriate device may be selected to obtain the desired emulsion particle size. Moreover, there is no restriction | limiting in particular about mixing conditions, The stirring rotation speed and stirring time which can obtain the target emulsion particle size can be set arbitrarily. Among these mixing apparatuses, the planetary stirring apparatus is preferably used because it can uniformly generate water droplets in the W / O emulsion and can arbitrarily set the average diameter within a wide range.

  In the production of the first monolith, various polymerization conditions for polymerizing the water-in-oil emulsion thus obtained can be selected depending on the type of monomer and the initiator system. For example, when azobisisobutyronitrile, benzoyl peroxide, potassium persulfate, or the like is used as a polymerization initiator, it can be heated and polymerized at 30 to 100 ° C. for 1 to 48 hours in a sealed container under an inert atmosphere. When hydrogen peroxide-ferrous chloride, sodium persulfate-sodium acid sulfite, etc. are used as initiators, polymerization can be carried out at 0-30 ° C. for 1-48 hours in a sealed container under an inert atmosphere. That's fine. After completion of the polymerization, the content is taken out and subjected to Soxhlet extraction with a solvent such as isopropanol to remove the unreacted monomer and the remaining surfactant to obtain a first monolith.

  The method for producing the first monolith ion exchanger is not particularly limited. In the first monolith production method, instead of the monomer not containing an ion exchange group, a monomer containing an ion exchange group, for example, the above ion Monolith ion exchange is performed in one step by polymerizing an oil-soluble monomer that does not contain an exchange group with a monomer having a cation exchange group such as a carboxylic acid group or a sulfonic acid group or an anion exchange group such as a quaternary ammonium group. And a method of polymerizing with a monomer not containing an ion exchange group to form a first monolith and then introducing an ion exchange group. Among these methods, the method of polymerizing using a monomer not containing an ion exchange group to form the first monolith and then introducing the ion exchange group makes it easy to control the porous structure of the monolith ion exchanger. It is preferable because quantitative introduction of ion exchange groups is possible.

  There is no restriction | limiting in particular as a method to introduce | transduce an ion exchange group into a 1st monolith, Well-known methods, such as a polymer reaction and graft polymerization, can be used. For example, as a method of introducing a quaternary ammonium group, if the monolith is a styrene-divinylbenzene copolymer or the like, a chloromethyl group is introduced with chloromethyl methyl ether or the like and then reacted with a tertiary amine for introduction; Monolith is produced by copolymerization of chloromethylstyrene and divinylbenzene and introduced by reacting with a tertiary amine; radical initiation group or chain transfer group is introduced into monolith, and N, N, N-trimethylammonium ethyl acrylate or N , N, N-trimethylammonium propylacrylamide; a method of grafting glycidyl methacrylate in the same manner and then introducing a quaternary ammonium group by functional group conversion. Among these methods, the method of introducing a quaternary ammonium group includes a method of introducing a chloromethyl group into a styrene-divinylbenzene copolymer with chloromethyl methyl ether and then reacting with a tertiary amine, or chloromethylstyrene. A method of producing a monolith by copolymerization with divinylbenzene and reacting with a tertiary amine is preferable in that the ion exchange groups can be introduced uniformly and quantitatively. Examples of anion exchange groups to be introduced include quaternary ammonium groups such as trimethylammonium group, triethylammonium group, tributylammonium group, dimethylhydroxyethylammonium group, dimethylhydroxypropylammonium group, methyldihydroxyethylammonium group, and tertiary sulfonium. Group, phosphonium group and the like. Further, for example, as a method for introducing a sulfonic acid group, if the monolith is a styrene-divinylbenzene copolymer or the like, a method of sulfonation using chlorosulfuric acid, concentrated sulfuric acid, or fuming sulfuric acid; And a method of grafting sodium styrene sulfonate or acrylamido-2-methylpropane sulfonic acid by introducing a chain transfer group into the skeleton surface or inside the skeleton; Similarly, after graft polymerization of glycidyl methacrylate, the sulfonic acid group is converted by functional group conversion. The method etc. which introduce | transduce are mentioned. Among these methods, the method of introducing sulfonic acid into the styrene-divinylbenzene copolymer using chlorosulfuric acid is preferable in that the ion exchange groups can be introduced uniformly and quantitatively. Examples of ion exchange groups to be introduced include cation exchange groups such as carboxylic acid groups, iminodiacetic acid groups, sulfonic acid groups, phosphoric acid groups, and phosphoric acid ester groups.

<Description of Second Monolith and Second Monolith Ion Exchanger>
In the platinum group metal catalyst of the present invention, the second monolith and the second monolith ion exchanger serving as a support for the platinum group metal particles are particle agglomerated monoliths having an average particle diameter of 1 to 50 μm in a wet state in water. Organic polymer particles aggregate to form a three-dimensionally continuous skeleton part, and between the skeletons, there are three-dimensionally continuous pores having an average diameter of 20 to 100 μm in a water-wet state. It is an organic porous body having a total pore volume of 1 to 5 ml / g. Further, the second monolith ion exchanger has an ion exchange group, an ion exchange capacity per volume in a water-wet state is 0.3 to 1.0 mg equivalent / ml, and the ion exchange group has the ion exchange group. A monolithic ion exchanger uniformly distributed in an organic porous ion exchanger.

  The basic structure of the second monolith and the second monolith ion exchanger is a three-dimensional structure in which organic polymer particles having an average particle diameter of 1 to 50 μm, preferably 1 to 30 μm in a wet state are aggregated. It is a particle aggregation type structure in which continuous skeleton parts are formed and three-dimensionally continuous pores having an average diameter of 20 to 100 μm, preferably 20 to 90 μm, between the skeletons in a water-wet state. The continuous pores become a flow path for liquid or gas. FIG. 2 shows an SEM photograph of a form example of the second monolith. In the second monolith shown in FIG. 2, organic polymer particles aggregate to form a three-dimensional continuous skeleton portion. It is a particle aggregation type structure having three-dimensionally continuous pores between them. If the average particle diameter of the organic polymer particles is less than 1 μm in the water-wet state, the average diameter of the continuous pores between the skeletons will be less than 20 μm in the water-wet state, which is not preferable. The contact between the treated water and the monolith or monolith ion exchanger becomes insufficient, and as a result, the hydrogen peroxide decomposition effect or the dissolved oxygen removal effect is lowered, which is not preferable. Further, if the average diameter of the three-dimensionally continuous pores existing between the skeletons is less than 20 μm in the water-wet state, it is not preferable because the pressure loss when the treated water is permeated increases. If the thickness exceeds 100 μm, the contact between the water to be treated and the monolith or monolith ion exchanger becomes insufficient, and the hydrogen peroxide decomposition characteristics or dissolved oxygen removal characteristics deteriorate, which is not preferable.

  In addition, the average particle diameter in the dry state of the organic polymer particle which comprises the frame | skeleton part of a 2nd monolith and a 2nd monolith ion exchanger is simply measured by using SEM. The average particle diameter of the organic polymer particles constituting the skeleton part of the second monolith in the water-wet state or the second monolith ion exchanger is the skeleton of the second monolith in the dry state or the second monolith ion exchanger. This is a value calculated by multiplying the average particle diameter of the organic polymer particles constituting the portion by the swelling rate. Specifically, first, an SEM photograph of an arbitrarily extracted portion of the cross section of the second monolith or the second monolith ion exchanger in a dry state is taken, and the diameter of the organic polymer particles of all particles in the SEM photograph is determined. The average particle size of the organic polymer particles in the dried second monolith or the second monolith ion exchanger is measured. Next, the average particle diameter of the organic polymer particles in the second monolith or the second monolith ion exchanger in the water wet state is calculated by multiplying the average particle diameter of the obtained organic polymer particles in the dry state by the swelling ratio. To do. For example, the diameter of the second monolith (or monolith ion exchanger) in the water wet state is x1 (mm), the second monolith (or monolith ion exchanger) in the water wet state is dried, and the resulting drying The diameter of the second monolith (or monolith ion exchanger) in the state is y1 (mm), and an SEM photograph of a cross section of the second monolith (or monolith ion exchanger) in the dry state is taken, in the SEM photograph If the average particle diameter when measuring the diameter of the organic polymer particles of all the particles is z1 (μm), the average particle of the organic polymer particles in the second monolith (or monolith ion exchanger) in a water-wet state The diameter (μm) is calculated by the following formula “average particle diameter of organic polymer particles (μm) = z1 × (x1 / y1) in the second monolith (or monolith ion exchanger) in a water-wet state” ”. . Further, the average particle diameter of the organic polymer particles in the second monolith in the dry state before the introduction of the ion exchange group, and the second monolith in the dry state when the ion exchange group is introduced into the second monolith in the dry state When the swelling ratio of the second monolith ion exchanger in the water wet state is known, the average particle diameter of the organic polymer particles in the second monolith in the dry state is multiplied by the swelling ratio to obtain the second wet water state second monolith. The average particle diameter of the organic polymer particles in the monolith ion exchanger can also be calculated.

  In addition, the average diameter of three-dimensionally continuous pores existing between the skeletons of the second monolith in the dry state or the three-dimensionally continuous voids existing between the skeletons of the second monolith ion exchanger in the dry state. The average diameter of the pores is obtained by the mercury intrusion method, and indicates the maximum value of the pore distribution curve obtained by the mercury intrusion method. The average diameter of the three-dimensionally continuous pores existing between the skeletons of the second monolith or the second monolith ion exchanger in the water wet state is the second monolith or the second monolith ion in the dry state. This is a value calculated by multiplying the average diameter of three-dimensionally continuous pores existing between the skeletons of the exchanger by the swelling rate. Specifically, the diameter of the second monolith (or monolith ion exchanger) in the water wet state is x2 (mm), and the second monolith (or monolith ion exchanger) in the water wet state is dried, The diameter of the resulting dried second monolith (or monolith ion exchanger) is y2 (mm), and this dried second monolith (or monolith ion exchanger) is measured by mercury porosimetry. If the average diameter of three-dimensionally continuous pores existing between the skeletons is z2 (μm), the three-dimensional ones existing between the skeletons of the second monolith (or monolith ion exchanger) in a water-wet state. The average diameter (μm) of the continuous pores in the three-dimensionally continuous pores existing between the skeletons of the second monolith (or monolith ion exchanger) in the water wet state (μm) ) = Z2 × (x2 y2) "is calculated by. In addition, the average diameter of three-dimensionally continuous pores existing between the skeletons of the second monolith in the dry state before the introduction of the ion exchange group, and when the ion exchange group is introduced into the second monolith in the dry state If the swelling ratio of the water-wet second monolith ion exchanger relative to the dry second monolith is known, then the average of the three-dimensional continuous pores present between the skeletons of the dry second monolith It is also possible to calculate the average diameter of three-dimensionally continuous pores existing between the skeletons of the second monolithic ion exchanger in the water wet state by multiplying the diameter by the swelling rate.

  The total pore volume per weight in the dry state of the second monolith and the second monolith ion exchanger is 1-5 ml / g. If the total pore volume is less than 1 ml / g, it is not preferable because the pressure loss at the time of passing water increases, and further, the amount of permeated water per unit cross-sectional area decreases, and the treatment capacity decreases. Absent. On the other hand, if the total pore volume exceeds 5 ml / g, the mechanical strength is lowered, and the monolith and the monolith ion exchanger are greatly deformed particularly when water is passed at a high flow rate.

  The pressure loss when water is permeated through the second monolith and the second monolith ion exchanger is the pressure loss when water is passed through a column packed with 1 m at a water flow velocity (LV) of 1 m / h ( Hereinafter, it is referred to as “differential pressure coefficient”.) 0.005 to 0.1 MPa / m · LV is preferable, and 0.005 to 0.05 MPa / m · LV is particularly preferable. If the differential pressure coefficient and the total pore volume are in the above ranges, when this is used as a catalyst, the contact area with the water to be treated is large, and the water to be treated can be smoothly circulated. Can be demonstrated.

  In the second monolith and the second monolith ion exchanger, the material of the skeleton portion is an organic polymer material having a crosslinked structural unit. That is, the organic polymer material has a constitutional unit composed of a vinyl monomer and a cross-linking agent structural unit having two or more vinyl groups in the molecule, and the polymer material comprises all the constitutions constituting the polymer material. It is preferable that 1 to 5 mol%, preferably 1 to 4 mol% of a crosslinked structural unit is contained with respect to the unit. When the cross-linking structural unit is less than 1 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, when it exceeds 5 mol%, the pore diameter that exists three-dimensionally continuously between the skeletons is reduced. Therefore, the pressure loss increases, which is not preferable.

  The type of the polymer material constituting the skeleton of the second monolith and the second monolith ion exchanger is not particularly limited. For example, styrene-based polymers such as polystyrene, poly (α-methylstyrene), polyvinylbenzyl chloride; polyethylene Polyolefins such as polypropylene; poly (halogenated polyolefins) such as polyvinyl chloride and polytetrafluoroethylene; nitrile polymers such as polyacrylonitrile; (meth) such as polymethyl methacrylate, polyglycidyl methacrylate, and polyethyl acrylate Acrylic polymers; styrene-divinylbenzene copolymer, vinylbenzyl chloride-divinylbenzene copolymer and the like. The polymer may be a polymer obtained by copolymerizing a single monomer and a crosslinking agent, or may be a polymer obtained by polymerizing a plurality of monomers and a crosslinking agent, and two or more kinds of polymers are blended. It may be a thing. Among these organic polymer materials, styrene-divinylbenzene copolymer is used because of its easy formation of particle aggregate structure, ease of ion exchange group introduction and high mechanical strength, and high stability against acid or alkali. Preferred materials include a polymer and a vinylbenzyl chloride-divinylbenzene copolymer.

  The ion exchange group introduced into the second monolith ion exchanger is the same as the ion exchange group introduced into the first monolith ion exchanger.

  In the second monolith ion exchanger, the introduced ion exchange groups are uniformly distributed not only on the surface of the porous body but also inside the skeleton of the porous body, as in the first monolith ion exchanger. Yes.

  The ion exchange capacity of the second monolith ion exchanger is 0.3 to 1.0 mg equivalent / ml per volume in a water-wet state. The second monolith ion exchanger can significantly increase the ion exchange capacity per volume while keeping the pressure loss low. If the ion exchange capacity per volume under water wet condition is in the above range, in the case of a monolith ion exchanger having an OH-type anion exchange group, the basicity in the vicinity of the catalyst support becomes high, and hydrogen peroxide decomposition characteristics Or the dissolved oxygen removal property becomes high. In addition, when the ion exchange capacity per volume in a water-wet state exceeds 1.0 mg equivalent / ml, the volume change of swelling and shrinkage of the monolith ion exchanger due to the change of the ion form tends to be too large. In addition, the ion exchange capacity per weight in the dry state of the second monolith ion exchanger is not particularly limited, but since the ion exchange groups are uniformly introduced to the surface of the porous body and the inside of the skeleton, A value of 5 mg equivalent / g is shown.

<Method for Producing Second Monolith and Second Monolith Ion Exchanger>
As a method for producing the second monolith, a method of obtaining a second monolith by mixing a vinyl monomer, a specific amount of a crosslinking agent, an organic solvent and a polymerization initiator and polymerizing them in a stationary state can be mentioned. It is done.

  The vinyl monomer used for the production of the second monolith is not particularly limited as long as it is a lipophilic monomer containing a polymerizable vinyl group in the molecule and having high solubility in an organic solvent. Specific examples of these vinyl monomers include styrene monomers such as styrene, α-methylstyrene, vinyl toluene and vinyl benzyl chloride; α-olefins such as ethylene, propylene, 1-butene and isobutene; butadiene, isoprene and chloroprene. Diene monomers; Halogenated olefins such as vinyl chloride, vinyl bromide, vinylidene chloride and tetrafluoroethylene; Nitrile monomers such as acrylonitrile and methacrylonitrile; Vinyl esters such as vinyl acetate and vinyl propionate; Methyl acrylate and Acrylic Ethyl acetate, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate, ethyl methacrylate, propyl methacrylate, butyl methacrylate, 2-ethylhexyl methacrylate, cyclohexyl methacrylate And (meth) acrylic monomers such as benzyl methacrylate and glycidyl methacrylate. These monomers are used singly or in combination of two or more. The vinyl monomer preferably used is a styrenic monomer such as styrene or vinyl benzyl chloride.

  The cross-linking agent used for the production of the second monolith preferably contains at least two polymerizable vinyl groups in the molecule and has high solubility in an organic solvent. Specific examples of the crosslinking agent include divinylbenzene, divinylnaphthalene, divinylbiphenyl, ethylene glycol dimethacrylate, trimethylolpropane triacrylate, butanediol diacrylate, and the like. These crosslinking agents are used singly or in combination of two or more. Preferred cross-linking agents are aromatic polyvinyl compounds such as divinylbenzene, divinylnaphthalene and divinylbiphenyl because of their high mechanical strength and stability to hydrolysis. The amount of crosslinking agent used ({crosslinking agent / (vinyl monomer + crosslinking agent)} × 100) relative to the total amount of vinyl monomer and crosslinking agent is 1 to 5 mol%, preferably 1 to 4 mol%. The use amount of the crosslinking agent has a great influence on the porous structure of the resulting monolith, and if the use amount of the crosslinking agent exceeds 5 mol%, the size of the continuous pores formed between the skeletons is preferably reduced. Absent. On the other hand, when the amount of the crosslinking agent used is less than 1 mol%, the mechanical strength of the monolith is insufficient, and the monolith is greatly deformed when water is passed or the monolith is destroyed.

  The organic solvent used for the production of the second monolith is an organic solvent that dissolves the vinyl monomer and the crosslinking agent but does not dissolve the polymer formed by polymerization of the vinyl monomer, in other words, for the polymer formed by polymerization of the vinyl monomer. It is a poor solvent. Since the organic solvent varies greatly depending on the type of vinyl monomer, it is difficult to list general specific examples. For example, when the vinyl monomer is styrene, the organic solvent includes methanol, ethanol, propanol, butanol, Hexanol, cyclohexanol, octanol, 2-ethylhexanol, decanol, dodecanol, alcohols such as ethylene glycol, tetramethylene glycol, glycerin; chain ethers such as diethyl ether, ethylene glycol dimethyl ether; hexane, octane, decane, dodecane, etc. And the like. Among these, alcohols are preferable because the particle aggregation structure is easily formed by stationary polymerization and the three-dimensional continuous pores are increased. Moreover, even if it is a good solvent of polystyrene like benzene and toluene, it is used with the said poor solvent, and when the usage-amount is small, it is used as an organic solvent.

  As the polymerization initiator used for the production of the second monolith, a compound that generates radicals by heat and light irradiation is preferable. The polymerization initiator is preferably oil-soluble. Specific examples of the polymerization initiator include 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2,2′-azobis (2-methylbutyronitrile). Nitrile), 2,2'-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2'-azobisisobutyrate, 4,4'-azobis (4-cyanovaleric acid), 1,1 ' -Azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, ammonium persulfate, tetramethylthiuram disulfide and the like. The amount of polymerization initiator used varies greatly depending on the type of monomer, polymerization temperature, etc., but the amount of polymerization initiator used relative to the total amount of vinyl monomer and crosslinking agent ({polymerization initiator / (vinyl monomer + crosslinking agent)} × 100) is about 0.01 to 5 mol%.

  In the production of the second monolith, various conditions can be selected as polymerization conditions depending on the type of monomer and the type of initiator. For example, when 2,2'-azobis (isobutyronitrile), 2,2'-azobis (2,4-dimethylvaleronitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, etc. are used as initiators In a sealed container under an inert atmosphere, heat polymerization may be performed at 30 to 100 ° C. for 1 to 48 hours. After completion of the polymerization, the contents are taken out and extracted with a solvent such as acetone to obtain a second monolith for the purpose of removing unreacted vinyl monomer and organic solvent.

  In the production of the second monolith, if the polymerization of the vinyl monomer dissolved in the organic solvent proceeds fast, organic polymer particles with an average particle diameter of 1 μm settle and aggregate to form a three-dimensional continuous skeleton. Can be made. The conditions under which the polymerization of the vinyl monomer proceeds rapidly vary depending on the vinyl monomer, the crosslinking agent, the polymerization initiator, the polymerization temperature, etc., but cannot be determined unconditionally, but increase the crosslinking agent, increase the monomer concentration, increase the temperature, etc. is there. Taking such polymerization conditions into consideration, the polymerization conditions for aggregating organic polymer particles having an average particle diameter of 1 to 50 μm may be appropriately determined. In addition, in order to form three-dimensionally continuous pores having an average diameter of 20 to 100 μm between the skeletons, as described above, the amount of crosslinking agent used should be a specific amount with respect to the total amount of vinyl monomer and crosslinking agent. That's fine. Moreover, in order to set the total pore volume of the monolith to 1 to 5 ml / g, depending on the vinyl monomer, the crosslinking agent, the polymerization initiator, the polymerization temperature, etc. If the amount of organic solvent used relative to the total amount used ({organic solvent / (organic solvent + monomer + crosslinking agent)} × 100) is polymerized under conditions such as 30 to 80% by weight, preferably 40 to 70% by weight Good.

  As a method for producing the second monolith ion exchanger, in the above-mentioned method for producing the second monolith, a monomer containing an ion exchange group, for example, a vinyl monomer not containing an ion exchange group, a carboxylic acid group, a sulfonic acid group Polymerization using a monomer into which an anion exchange group such as a cation exchange group or a quaternary ammonium group is introduced to form a monolith ion exchanger in one step, polymerization using a vinyl monomer that does not contain an ion exchange group And forming a second monolith, and then introducing an ion exchange group.

  The method for introducing ion exchange groups into the second monolith is the same as the method for introducing ion exchange groups into the first monolith.

<Description of Third Monolith and Third Monolith Ion Exchanger>
In the platinum group metal-supported catalyst of the present invention, the third monolith and the third monolith ion exchanger, which serve as a support for the platinum group metal particles, have bubble-like macropores overlapped with each other, and the overlapped portion has an average diameter in a wet state. In a SEM image of a continuous macropore structure having an opening of 30 to 300 μm, a total pore volume in a dry state of 0.5 to 5 ml / g, and a cut surface of the continuous macropore structure (dry body), It is an organic porous body whose skeleton part area which appears in a cross section is 25 to 50% in the image region. The third monolith ion exchanger has an ion exchange group, an ion exchange capacity per volume in a water-wet state is 0.4 to 1.0 mg equivalent / ml, and the ion exchange group is organic. It is a monolithic ion exchanger that is uniformly distributed in the porous ion exchanger.

  In the third monolith and the third monolith ion exchanger, bubble-shaped macropores are overlapped with each other, and the overlapping portion is wet with water and has an average diameter of 30 to 300 μm, preferably 30 to 200 μm, particularly preferably 40 to 100 μm. It is a continuous macropore structure that becomes (mesopore). FIG. 3 shows an SEM photograph of an example of the form of the third monolith. The third monolith shown in FIG. 3 has a large number of bubble-like macropores, and the bubble-like macropores overlap each other. The overlapping portion is a continuous macropore structure in which a common opening (mesopore) is formed, and most of the structure is an open pore structure. If the average diameter of the openings in the water-wet state is less than 30 μm, the pressure loss at the time of passing water increases, which is not preferable. Alternatively, the contact between the monolith ion exchanger and the supported platinum group metal particles becomes insufficient, and as a result, the hydrogen peroxide decomposition characteristic or the dissolved oxygen removal characteristic is deteriorated.

  In addition, the average diameter of the opening of the third monolith in the dry state, the average diameter of the opening of the third monolith ion exchanger in the dry state, and obtained in step I relating to the third monolith manufacturing method described below, The average diameter of the openings of the third monolith intermediate (3) in the dry state is measured by the mercury intrusion method. Further, the average diameter of the openings of the third monolith or the third monolith ion exchanger in the water-wet state is set to the average diameter of the openings of the third monolith or the third monolith ion exchanger in the dry state. It is a value calculated by multiplication. Specifically, the diameter of the third monolith (or monolith ion exchanger) in the water wet state is x1 (mm), and the third monolith (or monolith ion exchanger) in the water wet state is dried, The diameter of the obtained third monolith (or monolith ion exchanger) in the dry state is y1 (mm), and this third monolith (or monolith ion exchanger) in the dry state is measured by a mercury intrusion method. Assuming that the average diameter of the opening is z1 (μm), the average diameter (μm) of the third monolith (or monolith ion exchanger) in the water wet state is expressed by the following formula: “third monolith in the water wet state”. (Or average diameter (μm) = z1 × (x1 / y1)) of openings of (or monolith ion exchanger) ”. In addition, the average diameter of the opening of the third monolith in the dry state before the introduction of the ion exchange group and the water wet state relative to the third monolith in the dry state when the ion exchange group is introduced into the third monolith in the dry state When the swelling ratio of the third monolith ion exchanger is known, the average diameter of the third monolith ion exchanger in the water wet state is obtained by multiplying the average diameter of the opening of the third monolith in the dry state by the swelling ratio. The diameter can also be calculated.

  In the third monolith and the third monolith ion exchanger, in the SEM image of the cut surface of the continuous macropore structure (dry body), the skeleton part area appearing in the cross section is 25 to 50%, preferably 25 in the image region. ~ 45%. When the area of the skeletal part appearing in the cross section is less than 25% in the image area, the skeleton becomes a thin skeleton, the mechanical strength is lowered, and the monolith or the monolith ion exchanger is greatly deformed particularly when water is passed at a high flow rate. This is not preferable. Furthermore, the contact efficiency between the water to be treated and the monolith or monolith ion exchanger and the platinum group metal particles supported thereon is lowered, which is not preferable because the catalytic effect is lowered, and when it exceeds 50%, the skeleton becomes too thick, Since the pressure loss at the time of water flow increases, it is not preferable.

  The conditions for obtaining the SEM image may be any conditions as long as the skeleton part that appears in the cross section of the cut surface appears clearly. For example, the magnification is 100 to 600, and the photographic area is about 150 mm × 100 mm. In the SEM observation, the third monolith or the third monolith ion exchanger excluding subjectivity is photographed at three or more, preferably five or more, at different positions or positions photographed at an arbitrary position of the cut surface of the third monolith ion exchanger. This should be done with images. The third monolith or the third monolith ion exchanger to be cut is in a dry state for use in an electron microscope. The skeleton part of the cut surface in the SEM image will be described with reference to FIGS. FIG. 4 is a transcribed skeleton that appears as a cross section of the SEM photograph of FIG. In FIGS. 3 and 4, what is generally indeterminate and shown in cross section is the “skeleton part (reference numeral 12)” in the present invention, the circular hole shown in FIG. 3 is an opening (mesopore), and A relatively large curvature or curved surface is a macropore (reference numeral 13 in FIG. 4). The skeleton part area appearing in the cross section of FIG. 4 is 28% in the rectangular image region 11. Thus, the skeleton can be clearly determined.

  In the SEM image, the method for measuring the area of the skeletal part appearing in the cross section of the cut surface is not particularly limited, and after specifying the skeletal part by performing known computer processing or the like, calculation by automatic calculation or manual calculation by a computer or the like A method is mentioned. The manual calculation includes a method in which an indefinite shape is replaced with an aggregate such as a quadrangle, a triangle, a circle, or a trapezoid, and the areas are obtained by stacking them.

  The total pore volume per weight of the third monolith and the third monolith ion exchanger in the dry state is 0.5 to 5 ml / g, preferably 0.8 to 4 ml / g. If the total pore volume is less than 0.5 ml / g, the pressure loss during water flow will increase, which is not preferable. Further, the amount of permeated fluid per unit cross-sectional area decreases, and the processing capacity decreases. Therefore, it is not preferable. On the other hand, if the total pore volume exceeds 5 ml / g, the mechanical strength is lowered, and the monolith or monolith ion exchanger is greatly deformed particularly when water is passed at a high flow rate. Furthermore, since the contact efficiency between the water to be treated, the monolith or the monolith ion exchanger and the platinum group metal particles supported thereon is lowered, the catalytic effect is also lowered, which is not preferable.

  In addition, the pressure loss at the time of making water permeate | transmit the 3rd monolith and the 3rd monolith ion exchanger is when water is passed through the column filled with 1 m of the porous body at a water flow rate (LV) of 1 m / h. The pressure loss (hereinafter referred to as “differential pressure coefficient”) is in the range of 0.001 to 0.1 MPa / m · LV, particularly preferably 0.005 to 0.05 MPa / m · LV. . If the differential pressure coefficient and the total pore volume are in the above ranges, when this is used as a catalyst, the contact area with the water to be treated is large, and smooth distribution of the water to be treated is possible. Performance is demonstrated.

  In the third monolith and the third monolith ion exchanger, the material constituting the skeleton is an organic polymer material having a crosslinked structure. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.3 to 10 mol%, preferably 0.3 to 5 mol% of crosslinked structural units with respect to all structural units constituting the polymer material. It is preferable. If the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, if it exceeds 10 mol%, it may be difficult to introduce an ion exchange group.

  The type of the polymer material constituting the skeleton of the third monolith and the third monolith ion exchanger is not particularly limited. For example, polystyrene, poly (α-methylstyrene), polyvinyl toluene, polyvinyl benzyl chloride, polyvinyl biphenyl, Aromatic vinyl polymers such as polyvinyl naphthalene; polyolefins such as polyethylene and polypropylene; poly (halogenated polyolefins) such as polyvinyl chloride and polytetrafluoroethylene; nitrile polymers such as polyacrylonitrile; polymethyl methacrylate and polyglycidyl methacrylate And cross-linked polymers such as (meth) acrylic polymers such as polyethyl acrylate. The polymer may be a polymer obtained by copolymerizing a single vinyl monomer and a crosslinking agent, a polymer obtained by polymerizing a plurality of vinyl monomers and a crosslinking agent, or a blend of two or more types of polymers. It may be what was done. Among these organic polymer materials, it is easy to form a continuous macropore structure, when ion exchange groups are introduced, the ease of introduction of ion exchange groups and the high mechanical strength, and the high stability to acids or alkalis. Therefore, a crosslinked polymer of an aromatic vinyl polymer is preferable, and a styrene-divinylbenzene copolymer and a vinylbenzyl chloride-divinylbenzene copolymer are particularly preferable materials.

  The ion exchange group introduced into the third monolith ion exchanger is the same as the ion exchange group introduced into the first monolith ion exchanger.

  In the third monolith ion exchanger, the introduced ion exchange groups are uniformly distributed not only on the surface of the porous body but also inside the skeleton of the porous body.

  The third monolith ion exchanger has an ion exchange capacity per volume in a water-wet state of 0.4 to 1.0 mg equivalent / ml. The third monolith ion exchanger can further increase the opening diameter and thicken the skeleton of the continuous macropore structure (thicken the skeleton wall), so that the pressure loss per volume can be kept low. The ion exchange capacity can be dramatically increased. If the ion exchange capacity per volume under water wet condition is in the above range, in the case of a monolith ion exchanger having an OH-type anion exchange group, the basicity in the vicinity of the catalyst support becomes high, and hydrogen peroxide decomposition characteristics Or the dissolved oxygen removal property becomes high. In addition, when the ion exchange capacity per volume in a water-wet state exceeds 1.0 mg equivalent / ml, the volume change of swelling and shrinkage of the monolith ion exchanger due to the change of the ion form tends to be too large. The ion exchange capacity per weight of the third monolith ion exchanger is not particularly limited. However, since the ion exchange groups are uniformly introduced to the surface of the porous body and the inside of the skeleton, 3.5 to 4. 5 mg equivalent / g.

<Method for Producing Third Monolith and Third Monolith Ion Exchanger>
The third monolith prepares a water-in-oil emulsion by stirring a mixture of oil-soluble monomer, surfactant and water that does not contain ion exchange groups, and then polymerizes the water-in-oil emulsion to form a total pore. Step I for obtaining a monolithic organic porous intermediate (hereinafter also referred to as monolith intermediate (3)) having a continuous macropore structure having a volume of 5 to 16 ml / g, vinyl monomer, at least two or more in one molecule Obtained in Steps II and II of preparing a mixture comprising an organic solvent and a polymerization initiator that dissolves the vinyl monomer and the vinyl monomer and the crosslinking agent, but does not dissolve the polymer formed by polymerization of the vinyl monomer. The mixture was allowed to stand and polymerized in the presence of the monolith intermediate (3) obtained in the step I, and the mixture had a skeleton thicker than the skeleton of the monolith intermediate (3). III to obtain a monolithic, obtained by performing.

  In the third method for producing a monolith, the step I may be performed according to the method described in JP-A-2002-306976.

  In the production of the monolith intermediate (3) in the step I according to the third monolith production method, examples of the oil-soluble monomer containing no ion exchange group include a carboxylic acid group, a sulfonic acid group, and a quaternary ammonium group. Examples thereof include an oleophilic monomer that does not contain an ion exchange group and has low solubility in water. Preferable examples of these monomers include styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, divinyl benzene, ethylene, propylene, isobutene, butadiene, ethylene glycol dimethacrylate, and the like. These monomers can be used singly or in combination of two or more. However, a crosslinkable monomer such as divinylbenzene or ethylene glycol dimethacrylate is selected as at least one component of the oil-soluble monomer, and the content thereof is 0.3 to 10 mol% in the total oil-soluble monomer, preferably 0.3 to 5 mol% is preferable because the amount of ion-exchange groups can be quantitatively introduced when ion-exchange groups are introduced.

  The surfactant used in step I according to the third monolith production method can form a water-in-oil (W / O) emulsion when an oil-soluble monomer containing no ion exchange group and water are mixed. If it is a thing, there will be no restriction in particular, sorbitan monooleate, sorbitan monolaurate, sorbitan monopalmitate, sorbitan monostearate, sorbitan trioleate, polyoxyethylene nonyl phenyl ether, polyoxyethylene stearyl ether, polyoxyethylene sorbitan Nonionic surfactants such as monooleate; Anionic surfactants such as potassium oleate, sodium dodecylbenzenesulfonate, dioctyl sodium sulfosuccinate; Cationic surfactants such as distearyldimethylammonium chloride; Lauryl dimethyl It can be used an amphoteric surfactant such as Rubetain. These surfactants can be used singly or in combination of two or more. The water-in-oil emulsion refers to an emulsion in which an oil phase is a continuous phase and water droplets are dispersed therein. The amount of the surfactant added may vary depending on the type of oil-soluble monomer and the size of the target emulsion particles (macropores), but it cannot be generally stated, but the total amount of oil-soluble monomer and surfactant Can be selected within a range of about 2 to 70%.

  Further, in the step I according to the third method for producing a monolith, a polymerization initiator may be used as necessary when forming the water-in-oil emulsion. As the polymerization initiator, a compound that generates radicals by heat and light irradiation is preferably used. The polymerization initiator may be water-soluble or oil-soluble. For example, azobisisobutyronitrile, azobisdimethylvaleronitrile, azobiscyclohexanenitrile, azobiscyclohexanecarbonitrile, benzoyl peroxide, persulfate Examples include potassium, ammonium persulfate, hydrogen peroxide-ferrous chloride, sodium persulfate-sodium acid sulfite, and tetramethylthiuram disulfide.

  As the mixing method for forming a water-in-oil emulsion by mixing an oil-soluble monomer not containing an ion exchange group, a surfactant, water, and a polymerization initiator in the step I according to the third monolith production method. There is no particular limitation, a method of mixing each component at once, an oil-soluble monomer, a surfactant, an oil-soluble component that is an oil-soluble polymerization initiator, and water or a water-soluble polymerization initiator that is water-soluble For example, a method of mixing each component separately after uniformly dissolving the components can be used. There is no particular limitation on the mixing apparatus for forming the emulsion, and a normal mixer, homogenizer, high-pressure homogenizer, or the like can be used, and an appropriate apparatus may be selected to obtain the desired emulsion particle size. Moreover, there is no restriction | limiting in particular about mixing conditions, The stirring rotation speed and stirring time which can obtain the target emulsion particle size can be set arbitrarily.

  The monolith intermediate (3) obtained in the step I according to the third monolith production method has a continuous macropore structure. When this coexists in the polymerization system, a porous structure having a thick skeleton with the structure of the monolith intermediate (3) as a mold is formed. The monolith intermediate (3) is an organic polymer material having a crosslinked structure. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.3 to 10 mol%, preferably 0.3 to 5 mol% of crosslinked structural units with respect to all the structural units constituting the polymer material. Is preferred. When the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. In particular, when the total pore volume is as large as 10 to 16 ml / g, in order to maintain a continuous macropore structure, it is preferable to contain 2 mol% or more of cross-linked structural units. On the other hand, if it exceeds 10 mol%, it may be difficult to introduce ion exchange groups, which is not preferable.

  In the step I relating to the third method for producing a monolith, the type of the polymer material of the monolith intermediate (3) is not particularly limited, and examples thereof include the same as the polymer material of the first monolith described above. Thereby, the same polymer can be formed in the skeleton of the monolith intermediate (3), and the skeleton can be thickened to obtain a third monolith having a uniform skeleton structure.

  The total pore volume per weight in the dry state of the monolith intermediate (3) obtained in Step I according to the third monolith production method is 5 to 16 ml / g, preferably 6 to 16 ml / g. . If the total pore volume is too small, the total pore volume of the monolith obtained after polymerizing the vinyl monomer becomes too small, and the pressure loss during fluid permeation increases, which is not preferable. On the other hand, if the total pore volume is too large, the structure of the monolith obtained after polymerizing the vinyl monomer deviates from the continuous macropore structure, which is not preferable. In order to make the total pore volume of the monolith intermediate (3) within the above numerical range, the ratio of monomer to water may be set to approximately 1: 5 to 1:20.

  In addition, in the monolith intermediate (3) obtained in step I according to the third method for producing a monolith, the average diameter of openings (mesopores), which is an overlapping portion of macropores and macropores, is 20 to 200 μm in a dry state. If the average diameter of the opening in the dry state is less than 20 μm, the opening diameter of the monolith and the monolith ion exchanger obtained after polymerizing the vinyl monomer becomes small, and the pressure loss during water passage increases. It is not preferable. On the other hand, if it exceeds 200 μm, the opening diameter of the monolith and monolith ion exchanger obtained after polymerizing the vinyl monomer becomes too large, and the contact between the water to be treated and the monolith and monolith ion exchanger becomes insufficient. As a result, the hydrogen peroxide decomposition characteristic or the dissolved oxygen removal characteristic deteriorates, which is not preferable. The monolith intermediate (3) preferably has a uniform structure with uniform macropore size and opening diameter, but is not limited to this, and the nonuniform macropore larger than the uniform macropore size in the uniform structure. May be scattered.

  The II step relating to the third monolith production method includes a vinyl monomer, a cross-linking agent having at least two vinyl groups in one molecule, and a polymer formed by polymerization of the vinyl monomer while dissolving the vinyl monomer and the cross-linking agent. Is a step of preparing a mixture comprising an insoluble organic solvent and a polymerization initiator. In addition, there is no order of I process and II process, II process may be performed after I process, and I process may be performed after II process.

  The vinyl monomer used in step II according to the third monolith production method is not particularly limited as long as it is a lipophilic vinyl monomer containing a polymerizable vinyl group in the molecule and having high solubility in an organic solvent. Although not, it is preferable to select a vinyl monomer that produces the same or similar polymer material as the monolith intermediate (3) that coexists in the polymerization system. Specific examples of these vinyl monomers include aromatic vinyl monomers such as styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, vinyl biphenyl and vinyl naphthalene; α-olefins such as ethylene, propylene, 1-butene and isobutene; Diene monomers such as butadiene, isoprene and chloroprene; halogenated olefins such as vinyl chloride, vinyl bromide, vinylidene chloride and tetrafluoroethylene; nitrile monomers such as acrylonitrile and methacrylonitrile; vinyl such as vinyl acetate and vinyl propionate Esters: methyl acrylate, ethyl acrylate, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate, ethyl methacrylate, propyl methacrylate, butyl methacrylate, 2-methacrylic acid 2- Hexyl, cyclohexyl methacrylate, benzyl methacrylate, and (meth) acrylic monomer of glycidyl methacrylate. These monomers can be used singly or in combination of two or more. The vinyl monomer preferably used is an aromatic vinyl monomer such as styrene or vinyl benzyl chloride.

  The addition amount of the vinyl monomer used in Step II according to the third monolith production method is 3 to 50 times, preferably 4 to 40 times, by weight with respect to the monolith intermediate (3) that coexists during polymerization. . If the amount of vinyl monomer added is less than 3 times that of the monolith intermediate, the resulting monolith skeleton (thickness of the wall of the monolith skeleton) cannot be increased, and when an ion exchange group is introduced, Since the ion exchange capacity per volume becomes small, it is not preferable. On the other hand, if the amount of vinyl monomer added exceeds 50 times, the opening diameter becomes small, and the pressure loss during water passage becomes large, which is not preferable.

  As the crosslinking agent used in Step II according to the third monolith production method, a crosslinking agent containing at least two polymerizable vinyl groups in the molecule and having high solubility in an organic solvent is preferably used. Specific examples of the crosslinking agent include divinylbenzene, divinylnaphthalene, divinylbiphenyl, ethylene glycol dimethacrylate, trimethylolpropane triacrylate, butanediol diacrylate, and the like. These crosslinking agents can be used singly or in combination of two or more. Preferred cross-linking agents are aromatic polyvinyl compounds such as divinylbenzene, divinylnaphthalene and divinylbiphenyl because of their high mechanical strength and stability to hydrolysis. The amount of the crosslinking agent used is preferably from 0.3 to 10 mol%, particularly preferably from 0.3 to 5 mol%, based on the total amount of the vinyl monomer and the crosslinking agent. When the amount of the crosslinking agent used is less than 0.3 mol%, the mechanical strength of the monolith is insufficient, which is not preferable. On the other hand, if it exceeds 10 mol%, the amount of ion-exchange groups introduced may decrease, which is not preferable. In addition, it is preferable to use the said crosslinking agent usage-amount so that it may become substantially equal to the crosslinking density of the monolith intermediate (3) coexisted at the time of vinyl monomer / crosslinking agent polymerization. If the amounts used of both are too large, the crosslink density distribution is biased in the produced monolith, and cracks are likely to occur during the ion exchange group introduction reaction.

  The organic solvent used in Step II of the third monolith production method is an organic solvent that dissolves the vinyl monomer and the crosslinking agent but does not dissolve the polymer formed by polymerization of the vinyl monomer, in other words, the vinyl monomer is polymerized. It is a poor solvent for the polymer produced. Since the organic solvent varies greatly depending on the type of vinyl monomer, it is difficult to list general specific examples. For example, when the vinyl monomer is styrene, the organic solvent includes methanol, ethanol, propanol, butanol, Alcohols such as hexanol, cyclohexanol, octanol, 2-ethylhexanol, decanol, dodecanol, ethylene glycol, propylene glycol, tetramethylene glycol, glycerin; diethyl ether, ethylene glycol dimethyl ether, cellosolve, methyl cellosolve, butyl cellosolve, polyethylene glycol, polypropylene Chain (poly) ethers such as glycol and polytetramethylene glycol; hexane, heptane, octane, isooctane, decane, dode Chain saturated hydrocarbons such as down, ethyl acetate, isopropyl acetate, cellosolve acetate, esters such as ethyl propionate. Moreover, even if it is a good solvent of polystyrene like a dioxane, THF, and toluene, when it is used with the said poor solvent and the usage-amount is small, it can be used as an organic solvent. These organic solvents are preferably used so that the concentration of the vinyl monomer is 30 to 80% by weight. If the amount of the organic solvent used deviates from the above range and the vinyl monomer concentration is less than 30% by weight, the polymerization rate is lowered, and the monolith structure after polymerization deviates from the range of the third monolith. On the other hand, if the vinyl monomer concentration exceeds 80% by weight, the polymerization may run away, which is not preferable.

  As the polymerization initiator used in Step II according to the third method for producing a monolith, a compound that generates radicals by heat or light irradiation is preferably used. The polymerization initiator is preferably oil-soluble. Specific examples of the polymerization initiator include 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2,2′-azobis (2-methylbutyro). Nitrile), 2,2′-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2′-azobisisobutyrate, 4,4′-azobis (4-cyanovaleric acid), 1,1 ′ -Azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, ammonium persulfate, tetramethylthiuram disulfide and the like. The amount of the polymerization initiator used varies greatly depending on the type of monomer, polymerization temperature, etc., but can be used in a range of about 0.01 to 5% with respect to the total amount of vinyl monomer and crosslinking agent.

  In step III according to the third method for producing a monolith, the mixture obtained in step II is allowed to stand, and polymerization is performed in the presence of the monolith intermediate (3) obtained in step I. This is a step of obtaining a third monolith having a skeleton thicker than the skeleton of the body (3). The monolith intermediate (3) used in Step III plays an extremely important role in creating the third monolith, and when the monolith intermediate (3) having a continuous macropore structure is present in the polymerization system, A third monolith is obtained.

In the third method for producing a monolith, the internal volume of the reaction vessel is not particularly limited as long as the monolith intermediate (3) is large enough to be present in the reaction vessel, and the monolith intermediate (3 ) May be any of those in which a gap is formed around the monolith in plan view and those in which the monolith intermediate (3) enters the reaction vessel without any gap. Of these, the thick monolith after polymerization is not pressed from the inner wall of the container and enters the reaction container without any gap, and the monolith is not distorted, and the reaction raw materials are not wasted and efficient. Even when the internal volume of the reaction vessel is large and there are gaps around the monolith after polymerization, the vinyl monomer and the crosslinking agent are adsorbed and distributed on the monolith intermediate (3). A particle aggregate structure is not generated in the gap portion inside.
In step III according to the third method for producing a monolith, the monolith intermediate (3) is placed in a state impregnated with the mixture (solution) in the reaction vessel. As described above, the blending ratio of the mixture obtained in Step II and the monolith intermediate (3) is 3 to 50 times by weight, preferably 4 to 4 times by weight with respect to the monolith intermediate (3). It is preferable to blend so as to be 40 times. Thereby, it is possible to obtain a third monolith having a thick skeleton while having an appropriate opening diameter. In the reaction vessel, the vinyl monomer and the crosslinking agent in the mixture are adsorbed and distributed on the skeleton of the monolith intermediate that has been allowed to stand, and polymerization proceeds in the skeleton of the monolith intermediate (3).

  In the step III according to the third monolith production method, various conditions are selected as the polymerization conditions depending on the type of monomer and the type of initiator. For example, when 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, etc. are used as initiators In a sealed container under an inert atmosphere, heat polymerization may be performed at 30 to 100 ° C. for 1 to 48 hours. By the heat polymerization, the vinyl monomer adsorbed and distributed on the skeleton of the monolith intermediate (3) and the crosslinking agent are polymerized in the skeleton to thicken the skeleton. After completion of the polymerization, the content is taken out and extracted with a solvent such as acetone to obtain a third monolith for the purpose of removing unreacted vinyl monomer and organic solvent.

  The third monolith ion exchanger is obtained by performing an IV step of introducing an ion exchange group into the third monolith, which is a thick organic porous material obtained in the step III.

  The method for introducing an ion exchange group into the third monolith is the same as the method for introducing an ion exchange group into the first monolith.

  The third monolith and the third monolith ion exchanger have high mechanical strength because they have a thick bone skeleton despite the remarkably large opening diameter.

<Description of Fourth Monolith and Fourth Monolith Ion Exchanger>
In the platinum group metal-supported catalyst of the present invention, the fourth monolith and the fourth monolith ion exchanger serving as the support for the platinum group metal particles have a cross-linking structural unit of 0.3 to 5.0 mol% in all the structural units. A three-dimensional continuous skeleton having an average thickness of 1 to 60 μm in a water-wet state and an average diameter of 10 to 100 μm in a water-wet state between the skeletons. It is a co-continuous structure composed of pores, and is an organic porous body having a total pore volume of 0.5 to 5 ml / g in a dry state. The fourth monolith ion exchanger has an ion exchange group, an ion exchange capacity per volume in a water-wet state is 0.3 to 1.0 mg equivalent / ml, and the ion exchange group is organic. It is a monolithic ion exchanger that is uniformly distributed in the porous ion exchanger.

  The fourth monolith and the fourth monolith ion exchanger have a three-dimensional continuous skeleton having an average thickness of 1 to 60 μm, preferably 3 to 58 μm, in a water-wet state, and an average diameter of water between the skeletons. It is a co-continuous structure composed of three-dimensionally continuous pores of 10 to 100 μm, preferably 15 to 90 μm, particularly preferably 20 to 80 μm. FIG. 5 shows an SEM photograph of an example of the fourth monolith, and FIG. 6 shows a schematic diagram of a co-continuous structure of the fourth monolith and the fourth monolith ion exchanger. As shown in the schematic diagram of FIG. 6, the co-continuous structure is a structure 10 in which a continuous skeleton phase 1 and a continuous vacancy phase 2 are intertwined and each of them is three-dimensionally continuous. The continuous pores 2 have higher continuity of the pores than the conventional open-cell type monolith and the particle aggregation type monolith, and the size thereof is not biased. Moreover, since the skeleton is thick, the mechanical strength is high.

  If the average diameter of the three-dimensionally continuous pores is less than 10 μm in a water-wet state, it is not preferable because the pressure loss during water flow increases, and if it exceeds 100 μm, the water to be treated and the monolith or monolith ion The contact with the exchanger becomes insufficient, and as a result, decomposition of hydrogen peroxide in the water to be treated or removal of dissolved oxygen becomes insufficient, which is not preferable. Moreover, when the average thickness of the skeleton is less than 1 μm in a wet state, the monolith or the monolith ion exchanger is greatly deformed when water is passed at a high flow rate, which is not preferable. Furthermore, the contact efficiency between the water to be treated and the monolith or monolith ion exchanger decreases, and the catalytic effect decreases, which is not preferable. On the other hand, if the thickness of the skeleton exceeds 60 μm, the skeleton becomes too thick and pressure loss during water passage increases, which is not preferable.

  The average diameter of the opening of the fourth monolith in the dry state, the average diameter of the opening of the fourth monolith ion exchanger in the dry state, and the dry state obtained in step I relating to the fourth monolith production method described below The average diameter of the openings of the fourth monolith intermediate (4) is measured by mercury porosimetry. In addition, the average diameter of the pores of the fourth monolith and the fourth monolith ion exchanger in the water-wet state is the vacancy of the fourth monolith in the dry state or the fourth monolith ion exchanger measured by mercury porosimetry. This is a value calculated by multiplying the average diameter of the holes by the swelling rate. Specifically, the diameter of the water monolithic fourth monolith (or monolith ion exchanger) is x1 (mm), and the water monolithic fourth monolith (or monolith ion exchanger) is dried, The diameter of the obtained fourth monolith (or monolith ion exchanger) in the dry state is y1 (mm), and the fourth monolith (or monolith ion exchanger) in the dry state is measured by a mercury intrusion method. Assuming that the average diameter of the pores is z1 (μm), the average diameter (μm) of the pores of the fourth monolith (or monolith ion exchanger) in the water wet state is expressed by the following formula: 4 monolith (or monolith ion exchanger) average diameter of pores (μm) = z1 × (x1 / y1) ”. Further, the average diameter of the pores of the fourth monolith in the dry state before the introduction of the ion exchange group, and the water wet state with respect to the fourth monolith in the dry state when the ion exchange group is introduced into the fourth monolith in the dry state If the swelling ratio of the fourth monolith ion exchanger is known, the average diameter of the pores of the fourth monolith in the dry state is multiplied by the swelling ratio to obtain the empty space of the fourth monolith ion exchanger in the water wet state. The average diameter of the holes can also be calculated. The average thickness of the fourth monolith and the skeleton of the fourth monolith ion exchanger in the water-wet state is determined by performing SEM observation of the fourth monolith in the dry state or the fourth monolith ion exchanger at least three times. This is a value calculated by measuring the thickness of the skeleton in the obtained image and multiplying the average value by the swelling ratio. Specifically, the diameter of the fourth monolith (or monolith ion exchanger) in the water wet state is x2 (mm), and the fourth monolith (or monolith ion exchanger) in the water wet state is dried, The diameter of the resulting dried fourth monolith (or monolith ion exchanger) is y2 (mm), and SEM observation of this dried fourth monolith (or monolith ion exchanger) is performed at least three times, When the thickness of the skeleton in the obtained image was measured and the average value was z2 (μm), the average of the skeleton of the continuous structure of the fourth monolith (or monolith ion exchanger) in a water-wet state The thickness (μm) is calculated by the following formula “average thickness (μm) = z2 × (x2 / y2) of the skeleton of the continuous structure of the fourth monolith (or monolith ion exchanger) in the water wet state”. The Further, the average thickness of the skeleton of the fourth monolith in the dry state before the introduction of the ion exchange group, and the water wet state with respect to the fourth monolith in the dry state when the ion exchange group is introduced into the fourth monolith in the dry state If the swelling ratio of the fourth monolith ion exchanger is known, the skeleton of the fourth monolith ion exchanger in the water-wet state is obtained by multiplying the average thickness of the skeleton of the fourth monolith in the dry state by the swelling ratio. It is also possible to calculate the average thickness. The skeleton has a rod-like shape and a circular cross-sectional shape, but may have a cross-section with a different diameter such as an elliptical cross-sectional shape. The thickness in this case is the average of the minor axis and the major axis.

  Further, the total pore volume per weight in the dry state of the fourth monolith and the fourth monolith ion exchanger is 0.5 to 5 ml / g. If the total pore volume is less than 0.5 ml / g, the pressure loss at the time of water flow is increased, which is not preferable. Further, the amount of permeated water per unit cross-sectional area is decreased, and the amount of treated water is decreased. Therefore, it is not preferable. On the other hand, if the total pore volume exceeds 5 ml / g, the mechanical strength is lowered, and the monolith or monolith ion exchanger is greatly deformed particularly when water is passed at a high flow rate. Furthermore, since the contact efficiency between the water to be treated and the monolith or monolith ion exchanger is lowered, the hydrogen peroxide decomposition effect or the dissolved oxygen removal effect is also lowered, which is not preferable. If the three-dimensional continuous pore size and total pore volume are within the above ranges, the contact with the water to be treated is extremely uniform, the contact area is large, and water can flow through under low pressure loss. Become.

  The pressure loss when water is allowed to permeate through the fourth monolith and the fourth monolith ion exchanger is the pressure when water is passed through a column filled with 1 m of a porous material at a water flow velocity (LV) of 1 m / h. In terms of loss (hereinafter referred to as “differential pressure coefficient”), it is in the range of 0.001 to 0.5 MPa / m · LV, particularly 0.005 to 0.1 MPa / m · LV. If the differential pressure coefficient and the total pore volume are in the above ranges, when this is used as a catalyst, the contact area with the water to be treated is large, and smooth distribution of the water to be treated is possible. Performance can be demonstrated.

  In the fourth monolith and the fourth monolith ion exchanger, the material constituting the skeleton is 0.3 to 5 mol%, preferably 0.5 to 3.0 mol% of a crosslinked structural unit in all the structural units. It is an aromatic vinyl polymer containing and is hydrophobic. If the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, if it exceeds 5 mol%, the structure of the porous body tends to deviate from the bicontinuous structure. There is no restriction | limiting in particular in the kind of aromatic vinyl polymer, For example, a polystyrene, poly ((alpha) -methylstyrene), polyvinyl toluene, polyvinyl benzyl chloride, polyvinyl biphenyl, polyvinyl naphthalene etc. are mentioned. The polymer may be a polymer obtained by copolymerizing a single vinyl monomer and a crosslinking agent, a polymer obtained by polymerizing a plurality of vinyl monomers and a crosslinking agent, or a blend of two or more types of polymers. It may be what was done. Among these organic polymer materials, a styrene-divinylbenzene copolymer is used because of its ease of forming a co-continuous structure, ease of introduction of ion-exchange groups, high mechanical strength, and high stability against acids or alkalis. And vinylbenzyl chloride-divinylbenzene copolymer is preferred.

  The ion exchange group introduced into the fourth monolith ion exchanger is the same as the ion exchange group introduced into the first monolith ion exchanger.

  In the fourth monolith ion exchanger, the introduced ion exchange groups are uniformly distributed not only on the surface of the porous body but also within the skeleton of the porous body.

  The fourth monolith ion exchanger has an ion exchange capacity of 0.3 to 1.0 mg equivalent / ml per volume in a water wet state. Since the fourth monolith ion exchanger has high continuity and uniformity of three-dimensionally continuous pores, the pressure loss does not increase so much even if the total pore volume is reduced. Therefore, it is possible to dramatically increase the ion exchange capacity per volume while keeping the pressure loss low. If the ion exchange capacity per volume is in the above range, in the case of a monolith ion exchanger having an OH-type anion exchange group, the basicity in the vicinity of the catalyst carrier is increased, and the hydrogen peroxide decomposition characteristics or dissolved oxygen removal characteristics are improved. Get higher. In addition, when the ion exchange capacity per volume in a water-wet state exceeds 1.0 mg equivalent / ml, the volume change of swelling and shrinkage of the monolith ion exchanger due to the change of the ion form tends to be too large. In addition, the ion exchange capacity per weight in the dry state of the fourth monolith ion exchanger is not particularly limited, but the ion exchange groups are uniformly introduced to the skeleton surface and the skeleton inside the porous body. 5 to 4.5 mg equivalent / g.

<Method for Manufacturing Fourth Monolith and Fourth Monolith Inion Exchanger>
The fourth monolith prepares a water-in-oil emulsion by stirring a mixture of oil-soluble monomer, surfactant and water that does not contain ion exchange groups, and then polymerizes the water-in-oil emulsion to form a total pore. Step I for obtaining a monolithic organic porous intermediate (hereinafter also referred to as monolith intermediate (4)) having a continuous macropore structure having a volume of more than 16 ml / g and 30 ml / g or less, an aromatic vinyl monomer, one In all oil-soluble monomers having at least two vinyl groups in the molecule, 0.3 to 5 mol% of the crosslinking agent, aromatic vinyl monomer and crosslinking agent are dissolved, but the aromatic vinyl monomer is polymerized to form. Preparation of a mixture consisting of an organic solvent in which the polymer does not dissolve and a polymerization initiator, Step II, Monolith intermediate obtained in Step I while the mixture obtained in Step II is allowed to stand ( Present operating polymerization under the), III to obtain a fourth monolith organic porous material is a co-continuous structure, obtained by performing.

  In the step I relating to the fourth method for producing a monolith, the step I for obtaining the monolith intermediate (4) may be performed according to the method described in JP-A-2002-306976.

  That is, in the step I according to the fourth method for producing a monolith, as the oil-soluble monomer containing no ion exchange group, for example, ion exchange such as a carboxylic acid group, a sulfonic acid group, a tertiary amino group, a quaternary ammonium group, etc. Examples thereof include a lipophilic monomer which does not contain a group and has low solubility in water. Specific examples of these monomers include aromatic vinyl monomers such as styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, vinyl biphenyl and vinyl naphthalene; α-olefins such as ethylene, propylene, 1-butene and isobutene; butadiene Diene monomers such as vinyl chloride, vinyl bromide, vinylidene chloride and tetrafluoroethylene; nitrile monomers such as acrylonitrile and methacrylonitrile; vinyl esters such as vinyl acetate and vinyl propionate Methyl acrylate, ethyl acrylate, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate, ethyl methacrylate, propyl methacrylate, butyl methacrylate, 2-ethyl methacrylate Sill, cyclohexyl methacrylate, benzyl methacrylate, and (meth) acrylic monomer of glycidyl methacrylate. Among these monomers, preferred are aromatic vinyl monomers such as styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, divinyl benzene and the like. These monomers can be used singly or in combination of two or more. However, a crosslinkable monomer such as divinylbenzene or ethylene glycol dimethacrylate is selected as at least one component of the oil-soluble monomer, and its content is 0.3 to 5 mol%, preferably 0.3 to the total oil-soluble monomer. 3 mol% is preferable because it is advantageous for forming a co-continuous structure.

  The surfactant used in step I according to the fourth monolith production method is the same as the surfactant used in step I according to the third monolith production method, and the description thereof is omitted.

  Further, in the step I according to the fourth method for producing a monolith, a polymerization initiator may be used as necessary when forming the water-in-oil emulsion. As the polymerization initiator, a compound that generates radicals by heat or light irradiation is preferably used. The polymerization initiator may be water-soluble or oil-soluble. For example, 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2 , 2′-azobis (2-methylbutyronitrile), 2,2′-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2′-azobisisobutyrate, 4,4′-azobis ( 4-cyanovaleric acid), 1,1'-azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, ammonium persulfate, tetramethylthiuram disulfide, hydrogen peroxide-ferrous chloride Sodium persulfate-sodium acid sodium sulfite and the like.

  As the mixing method for forming a water-in-oil emulsion by mixing an oil-soluble monomer that does not contain an ion exchange group, a surfactant, water, and a polymerization initiator in Step I according to the fourth method for producing a monolith. Is the same as the mixing method in the step I according to the third method for producing a monolith, and the description thereof is omitted.

  The monolith intermediate (4) obtained in step I according to the fourth method for producing a monolith is an organic polymer material having a crosslinked structure, preferably an aromatic vinyl polymer. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.3 to 5 mol%, preferably 0.3 to 3 mol% of crosslinked structural units with respect to all structural units constituting the polymer material. Is preferred. When the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, if it exceeds 5 mol%, the structure of the monolith tends to deviate from the co-continuous structure, which is not preferable. In particular, when the total pore volume is 16 to 20 ml / g, the cross-linking structural unit is preferably less than 3 mol% in order to form a co-continuous structure.

  In step I according to the fourth monolith production method, the type of the polymer material of the monolith intermediate (4) is the same as the type of the polymer material of the monolith intermediate (3) according to the third monolith production method. The description is omitted.

  The total pore volume per weight in the dry state of the monolith intermediate (4) obtained in step I according to the fourth method for producing a monolith is more than 16 ml / g and not more than 30 ml / g, preferably 16 ml / g. g and 25 ml / g or less. That is, this monolith intermediate (4) is basically a continuous macropore structure, but the opening (mesopore) that is the overlapping portion of the macropore and the macropore is remarkably large, so that the skeleton constituting the monolith structure is two-dimensional. It has a structure that is almost as close as possible to a one-dimensional rod-like skeleton from the wall surface. FIG. 7 shows an SEM photograph of a form example of the monolith intermediate (4), which has a skeleton close to a rod shape. When this coexists in the polymerization system, a porous body having a co-continuous structure is formed using the structure of the monolith intermediate (4) as a mold. If the total pore volume is too small, the monolith structure obtained after polymerizing the vinyl monomer is not preferable because the structure changes from a co-continuous structure to a continuous macropore structure, while if the total pore volume is too large, When the mechanical strength of the monolith obtained after polymerizing the vinyl monomer is reduced or an ion exchange group is introduced, the ion exchange capacity per volume is lowered, which is not preferable. In order to make the total pore volume of the monolith intermediate (4) within the above range, the ratio of monomer to water may be about 1:20 to 1:40.

  Moreover, as for the monolith intermediate body (4) obtained at the I process which concerns on the manufacturing method of the 4th monolith, the average diameter of the opening (mesopore) which is an overlap part of a macropore and a macropore is 5-100 micrometers in a dry state. When the average diameter of the openings is less than 5 μm in the dry state, the opening diameter of the monolith obtained after polymerizing the vinyl monomer is reduced, and the pressure loss during fluid permeation is increased, which is not preferable. On the other hand, if it exceeds 100 μm, the opening diameter of the monolith obtained after polymerizing the vinyl monomer becomes too large, and the contact between the water to be treated and the monolith or monolith ion exchanger becomes insufficient. Since decomposition characteristics or dissolved oxygen removal characteristics deteriorate, it is not preferable. The monolith intermediate (4) preferably has a uniform structure with a uniform macropore size and opening diameter, but is not limited to this, and the nonuniform macropore larger than the uniform macropore size in the uniform structure. May be scattered.

  Step II according to the fourth method for producing a monolith includes an aromatic vinyl monomer, a total oil-soluble monomer having at least two vinyl groups in one molecule, 0.3 to 5 mol% of a crosslinking agent, aromatic This is a step of preparing a mixture of an organic solvent and a polymerization initiator that dissolves the vinyl monomer and the crosslinking agent but does not dissolve the polymer formed by polymerization of the aromatic vinyl monomer. In addition, there is no order of I process and II process, II process may be performed after I process, and I process may be performed after II process.

  The aromatic vinyl monomer used in Step II according to the fourth method for producing a monolith is an oleophilic aromatic vinyl monomer that contains a polymerizable vinyl group in the molecule and has high solubility in an organic solvent. Although there is no particular limitation, it is preferable to select a vinyl monomer that produces the same or similar polymer material as the monolith intermediate (4) to be coexisted in the polymerization system. Specific examples of these vinyl monomers include styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, vinyl biphenyl, vinyl naphthalene and the like. These monomers can be used singly or in combination of two or more. Aromatic vinyl monomers preferably used are styrene, vinyl benzyl chloride and the like.

  The addition amount of the aromatic vinyl monomer used in Step II according to the fourth monolith production method is 5 to 50 times by weight, preferably 5 to 40 times by weight, relative to the monolith intermediate (4) to be coexisted during the polymerization. It is. If the amount of the aromatic vinyl monomer added is less than 5 times that of the monolith intermediate (4), the rod-like skeleton cannot be made thick, and when ion exchange groups are introduced, ions per volume after introduction of the ion exchange groups This is not preferable because the exchange capacity becomes small. On the other hand, if the amount of the aromatic vinyl monomer added exceeds 50 times, the diameter of the continuous pores becomes small and the pressure loss during water passage becomes large, which is not preferable.

  As the crosslinking agent used in Step II according to the fourth method for producing a monolith, a crosslinking agent containing at least two polymerizable vinyl groups in the molecule and having high solubility in an organic solvent is preferably used. Specific examples of the crosslinking agent include divinylbenzene, divinylnaphthalene, divinylbiphenyl, ethylene glycol dimethacrylate, trimethylolpropane triacrylate, butanediol diacrylate, and the like. These crosslinking agents can be used singly or in combination of two or more. Preferred cross-linking agents are aromatic polyvinyl compounds such as divinylbenzene, divinylnaphthalene and divinylbiphenyl because of their high mechanical strength and stability to hydrolysis. The amount of the crosslinking agent used is 0.3 to 5 mol%, particularly 0.3 to 3 mol%, based on the total amount of vinyl monomer and crosslinking agent (total oil-soluble monomer). When the amount of the crosslinking agent used is less than 0.3 mol%, it is not preferable because the mechanical strength of the monolith is insufficient. On the other hand, when the amount is too large, it is difficult to quantitatively introduce the ion exchange group when introducing the ion exchange group. Since it may become, it is not preferable. In addition, it is preferable to use the said crosslinking agent usage-amount so that it may become substantially equal to the crosslinking density of the monolith intermediate (4) coexisted at the time of vinyl monomer / crosslinking agent polymerization. If the amounts used of both are too large, the crosslink density distribution will be biased in the produced monolith, and when ion exchange groups are introduced, cracks are likely to occur during the ion exchange group introduction reaction.

  The organic solvent used in Step II according to the fourth monolith production method is an organic solvent that dissolves the aromatic vinyl monomer and the crosslinking agent but does not dissolve the polymer formed by the polymerization of the aromatic vinyl monomer. It is a poor solvent for a polymer produced by polymerization of an aromatic vinyl monomer. Since organic solvents vary greatly depending on the type of aromatic vinyl monomer, it is difficult to list general specific examples. For example, when the aromatic vinyl monomer is styrene, the organic solvents include methanol, ethanol, and propanol. , Butanol, hexanol, cyclohexanol, octanol, 2-ethylhexanol, decanol, dodecanol, propylene glycol, tetramethylene glycol and other alcohols; Poly) ethers; chain saturated hydrocarbons such as hexane, heptane, octane, isooctane, decane, dodecane, etc .; ethyl acetate, isopropyl acetate, cellosolve acetate, propionic acid Examples include esters such as chill. Moreover, even if it is a good solvent of polystyrene like a dioxane, THF, and toluene, when it is used with the said poor solvent and the usage-amount is small, it can be used as an organic solvent. These organic solvents are preferably used so that the concentration of the aromatic vinyl monomer is 30 to 80% by weight. When the amount of the organic solvent deviates from the above range and the aromatic vinyl monomer concentration is less than 30% by weight, it is preferable because the polymerization rate decreases or the monolith structure after polymerization deviates from the range of the fourth monolith. Absent. On the other hand, if the concentration of the aromatic vinyl monomer exceeds 80% by weight, the polymerization may run away, which is not preferable.

  The polymerization initiator used in Step II according to the fourth monolith production method is the same as the polymerization initiator used in Step II according to the third monolith production method, and the description thereof is omitted.

  In step III according to the fourth method for producing a monolith, the mixture obtained in step II is allowed to stand and polymerize in the presence of the monolith intermediate (4) obtained in step I. This is a step of changing the continuous macropore structure of the body (4) to a co-continuous structure to obtain a fourth monolith that is a co-continuous structure monolith. The monolith intermediate (4) used in the step III plays an extremely important role in creating a monolith having a novel structure of the present invention. As disclosed in JP-A-7-501140 and the like, when a vinyl monomer and a crosslinking agent are allowed to stand in a specific organic solvent in the absence of the monolith intermediate (4), a particle aggregation type monolith shape is obtained. An organic porous body is obtained. On the other hand, when a monolith intermediate (4) having a specific continuous macropore structure is present in the polymerization system as in the case of the fourth monolith, the structure of the monolith after the polymerization changes dramatically and the particle aggregation structure disappears. Thus, the fourth monolith having the above-described co-continuous structure is obtained. The reason for this has not been elucidated in detail, but when the monolith intermediate (4) does not exist, the crosslinked polymer produced by polymerization precipitates and precipitates in the form of particles to form a particle aggregate structure. On the other hand, when a porous body (intermediate) having a large total pore volume exists in the polymerization system, the vinyl monomer and the crosslinking agent are adsorbed or distributed from the liquid phase to the skeleton of the porous body, and polymerization is performed in the porous body. It is considered that the skeleton constituting the monolith structure progresses to change from a two-dimensional wall surface to a one-dimensional rod-like skeleton, thereby forming a fourth monolith having a co-continuous structure.

  In the fourth monolith manufacturing method, the internal volume of the reaction vessel is the same as the description of the internal volume of the reaction vessel according to the third monolith manufacturing method, and the description thereof is omitted.

  In step III according to the fourth method for producing a monolith, the monolith intermediate (4) is placed in a state impregnated with the mixture (solution) in the reaction vessel. The blending ratio of the mixture obtained in Step II and the monolith intermediate (4) is, as described above, 5 to 50 times the weight of the aromatic vinyl monomer added to the monolith intermediate (4), preferably It is suitable to mix 5 to 40 times. Thereby, it is possible to obtain a fourth monolith having a co-continuous structure in which pores of an appropriate size are three-dimensionally continuous and a thick skeleton is three-dimensionally continuous. In the reaction vessel, the aromatic vinyl monomer and the cross-linking agent in the mixture are adsorbed and distributed on the skeleton of the monolith intermediate (4) that is allowed to stand, and polymerization proceeds in the skeleton of the monolith intermediate (4).

  The polymerization conditions of the III step according to the fourth monolith production method are the same as the explanation of the polymerization conditions of the III step according to the third monolith production method, and the description thereof is omitted. By performing step III, a fourth monolith is obtained.

  The fourth monolith ion exchanger is obtained by performing an IV step for introducing an ion exchange group into the fourth monolith obtained in the step III.

  The method for introducing ion exchange groups into the fourth monolith is the same as the method for introducing ion exchange groups into the first monolith.

  The fourth monolith and the fourth monolith ion exchanger have high mechanical strength because they have a thick bone skeleton even though the size of three-dimensionally continuous pores is extremely large. In addition, since the fourth monolith ion exchanger has a thick skeleton, the ion exchange capacity per volume in a water-wet state can be increased, and the treated water can be passed for a long time at a low pressure and a large flow rate. It is.

<Description of Fifth Monolith and Fifth Monolith Ion Exchanger>
In the platinum group metal-supported catalyst of the present invention, the fifth monolith and the fifth monolith ion exchanger serving as a support for the platinum group metal particles include an organic porous body comprising a continuous skeleton phase and a continuous pore phase, It is a composite structure with a large number of particles having a diameter of 4 to 40 μm fixed on the skeleton surface of the porous body or a large number of protrusions having a size of 4 to 40 μm formed on the skeleton surface of the organic porous body. The organic porous body has an average pore diameter of 10 to 150 μm in a wet state of water and a total pore volume of 0.5 to 5 ml / g in a dry state. Further, the fifth monolith ion exchanger has an ion exchange group, and has an ion exchange capacity of 0.2 mg equivalent / ml or more per volume in a water-wet state, and the ion exchange group is an organic porous ion exchange. It is a monolithic ion exchanger that is uniformly distributed throughout the body.

  The fifth monolith and the fifth monolith ion exchanger include an organic porous body composed of a continuous skeleton phase and a continuous pore phase, and a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body. Alternatively, it is a composite structure with a large number of protrusions having a size of 4 to 40 μm formed on the skeleton surface of the organic porous body. In the present specification, “particle bodies” and “projections” may be collectively referred to as “particle bodies”.

  The continuous skeletal phase and the continuous pore phase of the fifth monolith and the fifth monolith ion exchanger are observed by SEM images. Examples of the basic structure of the fifth monolith and the fifth monolith ion exchanger include a continuous macropore structure and a co-continuous structure. The skeletal phase of the fifth monolith and the fifth monolith ion exchanger appears as a columnar continuum, a continuum of concave wall surfaces, or a composite thereof, and has a shape that is clearly different from particles and protrusions. belongs to.

  As a preferable structure of the fifth monolith and the fifth monolith ion exchanger, bubble-shaped macropores overlap each other, and the overlapping portion has a continuous macropore structure (hereinafter referred to as “opening” having an average diameter of 10 to 120 μm in a dry state). 5-1 monolith "), and a three-dimensional continuous skeleton having an average thickness of 0.8 to 40 µm in a dry state, and a tertiary having an average diameter of 8 to 80 µm in a dry state between the skeletons. Examples thereof include a co-continuous structure (hereinafter, also referred to as “second monolith”) composed of originally continuous pores. As the fifth monolith ion exchanger, a monolith ion exchanger in which an ion exchange group is introduced into the 5-1 monolith (hereinafter also referred to as “5-1 monolith ion exchanger”), In addition, a monolith ion exchanger in which an ion exchange group is introduced into the 5-2 monolith (hereinafter, also referred to as a “5-2 monolith ion exchanger”) is preferable.

  In the case of the 5-1 monolith and the 5-1 monolith ion exchanger, the 5-1 monolith and the 5-1 monolith ion exchanger have bubble-like macropores overlapping each other, and the overlapping portion is water. It is a continuous macropore structure that becomes an opening (mesopore) having an average diameter of 20 to 150 μm, preferably 30 to 150 μm, particularly preferably 35 to 150 μm in a wet state, and the inside of bubbles formed by the macropore and the opening (mesopore) It becomes a flow path. The continuous macropore structure is preferably a uniform structure having the same macropore size and aperture diameter, but is not limited to this, and the uniform structure is dotted with nonuniform macropores larger than the size of the uniform macropore. You may do. When the average diameter of the openings in the water wet state of the 5-1 monolith and the 5-1 monolith ion exchanger is less than 20 μm, it is not preferable because the pressure loss at the time of passing water becomes large. When the average diameter of the opening in the water-wetting state exceeds 150 μm, the contact between the water to be treated and the monolith or monolith ion exchanger and the supported platinum group metal particles becomes insufficient. Since the removal characteristic of dissolved oxygen will fall, it is not preferable.

  In addition, the average diameter of the opening of the fifth monolith in the dry state, the average diameter of the opening of the fifth monolith ion exchanger in the dry state, and obtained in step I according to the fifth monolith manufacturing method described below, The average diameter of the opening of the monolith intermediate (5) in the dry state indicates the maximum value of the pore distribution curve obtained by the mercury intrusion method.

  In addition, the average diameter of the opening of the 5-1 monolith or the 5-1 monolith ion exchanger in the water wet state is the opening of the 5-1 monolith or the 5-1 monolith ion exchanger in the dry state. This is a value calculated by multiplying the average diameter by the swelling ratio. Specifically, the diameter of the 5-1 monolith (or monolith ion exchanger) in the water wet state is x1 (mm), and the 5-1 monolith (or monolith ion exchanger) in the water wet state is x1 (mm). The dried 5-1 monolith (or monolith ion exchanger) has a diameter y1 (mm), and the dried 5-1 monolith (or monolith ion exchanger) is Assuming that the average diameter of the opening measured by the mercury intrusion method is z1 (μm), the average diameter (μm) of the opening of the 5-1 monolith (or monolith ion exchanger) in the water wet state is It is calculated by the formula “average diameter (μm) = z1 × (x1 / y1) of openings of the 5-1 monolith (or monolith ion exchanger) in a water-wet state”. Further, the average diameter of the opening of the 5-1 monolith in the dry state before the introduction of the ion exchange group, and the 5-1 in the dry state when the ion exchange group is introduced into the 5-1 monolith in the dry state. When the swelling ratio of the 5-1 monolith ion exchanger in the water wet state relative to the monolith is known, the average diameter of the opening of the 5-1 monolith in the dry state is multiplied by the swelling ratio to obtain the water wet state It is also possible to calculate the average diameter of the openings of the monolithic ion exchanger of 5-1.

  In the case of the 5-2 monolith and the 5-2 monolith ion exchanger, the 5-2 monolith and the 5-2 monolith ion exchanger have an average thickness of 1 to 50 μm in a wet state, preferably Is a co-continuous structure having a three-dimensionally continuous skeleton of 5 to 50 μm and a three-dimensionally continuous pore having an average diameter of 10 to 100 μm, preferably 10 to 90 μm in a water-wet state between the skeletons. is there. When the average diameter of the three-dimensionally continuous pores of the 5-2 monolith and the 5-2 monolith ion exchanger in a water-wet state is less than 10 μm, the pressure loss during water passage increases. In addition, when it exceeds 100 μm, the contact between the water to be treated and the monolith or monolith ion exchanger and the supported platinum group metal particles becomes insufficient. As a result, hydrogen peroxide decomposition characteristics or dissolved oxygen This is not preferable because the removal characteristics deteriorate. In addition, when the average thickness of the skeletons of the 5-2 monolith and the 5-2 monolith ion exchanger is less than 1 μm in a wet state of water, the mechanical strength is lowered, and water is passed at a particularly high flow rate. In this case, the monolith or the monolith ion exchanger is greatly deformed, which is not preferable. On the other hand, if the average thickness of the skeleton of the 5-2 monolith and the 5-2 monolith ion exchanger exceeds 50 μm in a wet state, the skeleton becomes too thick and the pressure loss during water passage increases. It is not preferable.

  The average diameter of the pores of the 5-2 monolith or the 5-2 monolith ion exchanger in the water-wet state is the dry 5-2 monolith or 5-2 measured by mercury porosimetry. This is a value calculated by multiplying the average diameter of the pores of the monolith ion exchanger by the swelling rate. Specifically, the diameter of the 5-2 monolith (or monolith ion exchanger) in the water wet state is x2 (mm), and the 5-2 monolith (or monolith ion exchanger) in the water wet state is. The diameter of the resulting dried 5-2 monolith (or monolith ion exchanger) is y2 (mm), and this dried 5-2 monolith (or monolith ion exchanger) is Assuming that the average diameter of the pores when measured by the mercury intrusion method was z2 (μm), the average diameter (μm) of the pores of the 5-2 monolith (or monolith ion exchanger) in the water-wet state Is calculated by the following formula “average diameter of pores (μm) = z2 × (x2 / y2) of the 5-2 monolith (or monolith ion exchanger) in a wet state of water”. Further, the average diameter of the pores of the 5-2 monolith in the dry state before the introduction of the ion exchange group and the 5-2 in the dry state when the ion exchange group is introduced into the 5-2 monolith in the dry state are introduced. If the swelling ratio of the 5-2 monolith ion exchanger in the water wet state relative to the monolith is determined by multiplying the average diameter of the pores of the dry monolith 5-2 by the swelling ratio, the water wet state It is also possible to calculate the average diameter of the pores of the 5-2 monolith ion exchanger.

  In addition, the average thickness of the skeleton of the 5-2 monolith or the 5-2 monolith ion exchanger in the water wet state is the dry 5-2 monolith or the 5-2 monolith ion exchanger. This is a value calculated by performing SEM observation at least three times, measuring the thickness of the skeleton in the obtained image, and multiplying the average value by the swelling ratio. Specifically, the diameter of the 5-2 monolith (or monolith ion exchanger) in the water-wet state is x3 (mm), and the 5-2 monolith (or monolith ion exchanger) in the water-wet state is x 3 (mm). The diameter of the resulting dried 5-2 monolith (or monolith ion exchanger) is y3 (mm), and the dried 5-2 monolith (or monolith ion exchanger) has a diameter of y3 (mm). SEM observation was performed at least three times, and the thickness of the skeleton in the obtained image was measured. If the average value was z3 (μm), the water-wetting state 5-2 monolith (or monolith ion exchange) The average thickness (μm) of the skeleton of the continuous structure of the body is the average thickness (μm) of the continuous structure of the 5-2 monolith (or monolith ion exchanger) in the water-wet state = Z3 × (x3 / y3) ” . Also, the average thickness of the skeleton of the 5-2 monolith in the dry state before the introduction of the ion exchange group, and the 5-2 in the dry state when the ion exchange group is introduced into the 5-2 monolith in the dry state. When the swelling ratio of the 5-2 monolith ion exchanger in the water wet state relative to the monolith of the water is known, the average thickness of the skeleton of the dry monolith 5-2 is multiplied by the swelling ratio to obtain the water wet state. It is also possible to calculate the average thickness of the skeleton of the 5-2 monolith ion exchanger. The skeleton has a rod-like shape and a circular cross-sectional shape, but may have a cross-section with a different diameter such as an elliptical cross-sectional shape. The thickness in this case is the average of the minor axis and the major axis.

  The average diameter of the pores of the fifth monolith and the fifth monolith ion exchanger in a wet state with water is 10 to 150 μm. In the case of the 5-1 monolith and the 5-1 monolith ion exchanger, the preferred value of the pore diameter in the wet state of the 5-1 monolith and the 5-1 monolith ion exchanger is 30 to 150 μm. In addition, in the case of the 5-2 monolith and the 5-2 monolith ion exchanger, the preferred value of the pore size in the water wet state of the 5-2 monolith and the 5-2 monolith ion exchanger is 10-90 μm.

  In the fifth monolith and the fifth monolith ion exchanger, the diameter of the particles and the size of the protrusions in a wet state are 4 to 40 μm, preferably 4 to 30 μm, and particularly preferably 4 to 20 μm. In the present invention, both the particles and the protrusions are observed as protrusions on the surface of the skeleton, and the particles observed are referred to as particles, and the protrusions that are not granular are protrusions. Called the body. FIG. 8 shows a schematic cross-sectional view of the protrusion. As shown in FIGS. 8A to 8E, the protrusions protruding from the skeleton surface 21 are protrusions 22, and the protrusions 22 are like protrusions 22a shown in FIG. The shape close | similar to a granular shape, a hemispherical thing like the protrusion 22b shown to (B), the thing like the rise | swell of the skeleton surface like the protrusion 22c shown to (C), etc. are mentioned. In addition, the protrusion 22 has a shape that is longer in the direction perpendicular to the skeleton surface 21 than in the plane direction of the skeleton surface 21 as in the protrusion 22d shown in FIG. There is a thing of the shape which protruded in the several direction like the protrusion 22e shown to (E). Further, the size of the protrusions is determined by the SEM image when observed by SEM, and indicates the length of the portion where the width of each protrusion is the largest in the SEM image. Further, FIG. 9 shows an SEM photograph of the fifth monolith embodiment, in which a large number of protrusions are formed on the skeleton surface of the organic porous body.

  In the fifth monolith and the fifth monolith ion exchanger, the proportion of 4 to 40 μm particles in a wet state in all particles is 70% or more, preferably 80% or more. In addition, the ratio which 4-40 micrometers particle bodies etc. occupy in the water wet state in all the particle bodies etc. points out the number ratio of 4-40 micrometers particle bodies etc. in the water wet state which occupy the number of all particle bodies. Further, the surface of the skeletal phase is covered by 40% or more, preferably 50% or more by the whole particles. In addition, the coverage ratio of the surface of the skeleton layer with all particles and the like refers to an area ratio on the SEM image when the surface is observed by SEM, that is, an area ratio when the surface is viewed in plan. If the size of the particle covering the wall surface or the skeleton deviates from the above range, the effect of improving the contact efficiency between the fluid and the skeleton surface of the monolith or monolith ion exchanger and the inside of the skeleton tends to be small. In addition, all the particulate bodies etc. are all the particulate bodies formed on the surface of the skeleton layer including all the particulate bodies and protrusions in the size range other than the 4-40 μm particulate bodies in the wet state. And a protrusion.

  The diameter or size of the fifth monolith and the particles attached to the skeleton surface of the fifth monolith ion exchanger in the water wet state is the SEM of the fifth monolith and the fifth monolith ion exchanger in the dry state. A value calculated by multiplying the diameter or size of the particles obtained by observing the image by the swelling ratio when the dried state becomes the water wet state, or the fifth monolith in the dried state before the introduction of the inion exchange group This is a value calculated by multiplying the diameter or size of the particle or the like obtained by observation of the SEM image by the swelling rate before and after the introduction of the ion exchange group. Specifically, the diameter of the fifth monolith (or monolith ion exchanger) in the water wet state is x4 (mm), and the fifth monolith (or monolith ion exchanger) in the water wet state is dried. The diameter of the resulting dried fifth monolith (or monolith ion exchanger) is y4 (mm), and in the SEM image when this dried fifth monolith (or monolith ion exchanger) is observed by SEM If the diameter or size of the particle body or the like is z4 (μm), the diameter or size (μm) of the particle body or the like of the fifth monolith (or monolith ion exchanger) in the water wet state is expressed by the following formula: It is calculated by “the diameter or size (μm) = z4 × (x4 / y4) of the particle body or the like of the fifth monolith (or monolith ion exchanger) in a water-wet state” ”. Then, the diameter or size of all particles observed in the SEM image of the fifth monolith (or monolith ion exchanger) in the dry state is measured, and one field of view SEM image based on the measured value. The diameter or size of the whole particle body in the wet state is calculated. SEM observation of this dried fifth monolith (or monolith ion exchanger) is performed at least three times, and the diameter or size of all particles in the SEM image in the water wet state is calculated over the entire visual field. Confirming whether particles or the like having a diameter or size of 4 to 40 μm are observed, and when confirmed in the entire visual field, on the skeleton surface of the fifth monolith (or monolith ion exchanger), It is determined that a particle or the like having a diameter or a size of 4 to 40 μm in a wet state is formed. Further, according to the above, the diameter or size in the water wet state of all particles in the SEM image is calculated for each visual field, and the particle size of 4 to 40 μm in the water wet state occupying in the whole particles for each visual field. When the proportion of the particles, etc. in the wet state in all the particles is 70% or more in the entire visual field, the fifth monolith (or monolith ion) is obtained. It is judged that the ratio of 4 to 40 μm particles in the wet state is 70% or more in the total particles formed on the skeleton surface of the exchanger. Further, according to the above, the coverage ratio of the surface of the skeletal layer with all particles in the SEM image was determined for each field of view, and the coverage ratio of the surface of the skeleton layer with all particles in all fields was 40% or more. In this case, it is determined that the ratio of the surface of the skeleton layer of the fifth monolith (or monolith ion exchanger) covered with all particles is 40% or more. In addition, the diameter or size of the particles of the fifth monolith in the dry state before the introduction of the ion exchange groups, and the water for the fifth monolith in the dry state when the ion exchange groups are introduced into the fifth monolith in the dry state. When the swelling rate of the fifth monolith ion exchanger in the wet state is known, the diameter or size of the particles of the fifth monolith in the dry state is multiplied by the swelling rate to obtain the fifth moisture in the water wet state. Calculate the diameter or size of the monolith ion exchanger particles, etc., and in the same way as above, the diameter or size of the water monolithic fifth monolith ion exchanger particles, etc. In addition, the proportion of particles of 4 to 40 μm, etc., in the wet state of water, and the coating ratio of the surface of the skeleton layer with the particles can be determined.

  In the fifth monolith and the fifth monolith ion exchanger, if the coverage of the surface of the skeleton phase by the particle body or the like is less than 40%, the water to be treated and the inside of the skeleton of the monolith or monolith ion exchanger and the skeleton surface The effect of improving the contact efficiency tends to be small. Examples of the method for measuring the coverage with the particulates include an image analysis method using SEM images of the fifth monolith and the fifth monolith ion exchanger.

  The total pore volume per weight of the fifth monolith and the fifth monolith ion exchanger in the dry state is 0.5 to 5 ml / g, preferably 0.8 to 4 ml / g. If the total pore volume of the monolith and the monolith ion exchanger is less than 0.5 ml / g, it is not preferable because the pressure loss during water flow increases, and the amount of permeated fluid per unit cross-sectional area decreases. This is not preferable because the processing capacity is lowered. On the other hand, when the total pore volume of the monolith and the monolith ion exchanger exceeds 5 ml / g, the mechanical strength is lowered, and the monolith or the monolith ion exchanger is greatly deformed particularly when water is passed at a high flow rate. Therefore, it is not preferable. Furthermore, since the contact efficiency between the water to be treated, the monolith or the monolith ion exchanger and the platinum group metal particles supported thereon is lowered, the catalytic effect is also lowered, which is not preferable.

  In addition, the pressure loss at the time of making water permeate | transmit the 5th monolith and the 5th monolith ion exchanger is when water is passed through the column filled with 1 m of the porous body at a water flow rate (LV) of 1 m / h. The pressure loss (hereinafter referred to as “differential pressure coefficient”) is in the range of 0.005 to 0.1 MPa / m · LV, particularly preferably 0.005 to 0.05 MPa / m · LV. . If the differential pressure coefficient and the total pore volume are in the above ranges, when this is used as a catalyst, the contact area with the water to be treated is large, and smooth distribution of the water to be treated is possible. Performance can be demonstrated.

  In the fifth monolith and the fifth monolith ion exchanger, the material constituting the skeleton phase of the continuous pore structure is an organic polymer material having a crosslinked structure. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.3 to 10 mol%, preferably 0.3 to 5 mol% of crosslinked structural units with respect to all structural units constituting the polymer material. It is preferable. When the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, when it exceeds 10 mol%, when an ion exchange group is introduced, it is difficult to introduce the ion exchange group, Since the introduction amount may decrease, it is not preferable.

  There is no restriction | limiting in particular in the kind of polymer material used by manufacture of a 5th monolith, For example, aromatic vinyl polymers, such as a polystyrene, poly ((alpha) -methylstyrene), polyvinyl toluene, polyvinyl benzyl chloride, polyvinyl biphenyl, polyvinyl naphthalene; Polyolefins such as polyethylene and polypropylene; poly (halogenated polyolefins) such as polyvinyl chloride and polytetrafluoroethylene; nitrile polymers such as polyacrylonitrile; poly (methyl methacrylate, polyglycidyl methacrylate, poly (ethyl acrylate), etc. ) Crosslinked polymers such as acrylic polymers. The polymer may be a polymer obtained by copolymerizing a single vinyl monomer and a crosslinking agent, a polymer obtained by polymerizing a plurality of vinyl monomers and a crosslinking agent, or a blend of two or more types of polymers. It may be what was done. Among these organic polymer materials, the cross-linking of aromatic vinyl polymers is facilitated by the ease of forming a continuous pore structure, the ease of introducing ion exchange groups and the high mechanical strength, and the high stability to acids and alkalis A polymer is preferable, and a styrene-divinylbenzene copolymer and a vinylbenzyl chloride-divinylbenzene copolymer are particularly preferable materials.

  In the fifth monolith and the fifth monolith ion exchanger, the material constituting the skeleton phase of the organic porous body and the particles formed on the surface of the skeleton phase are of the same material in which the same structure is continuous, The thing of the material from which a mutually different structure | tissue which is not the same is different is mentioned. For materials with different structures with different continuous structures, such as materials with different types of vinyl monomers, materials with different blending ratios even if the types of vinyl monomers and crosslinking agents are the same, etc. Is mentioned.

  The ion exchange group introduced into the fifth monolith ion exchanger is the same as the ion exchange group introduced into the first monolith ion exchanger.

  In the fifth monolith ion exchanger, the introduced ion exchange groups are uniformly distributed not only on the surface of the organic porous body but also within the skeleton of the organic porous body. When the ion exchange groups are uniformly distributed not only on the surface of the fifth monolith ion exchanger but also inside the skeleton, the physical and chemical properties of the surface and the inside can be made uniform, so that the swelling and shrinkage The durability against is improved.

  The fifth monolith ion exchanger has an ion exchange capacity of 0.2 mg equivalent / ml or more, preferably 0.3 to 1.8 mg equivalent / ml per volume when wet in water. If the ion exchange capacity per volume of the fifth monolith ion exchanger is in the above range, in the case of a monolith ion exchanger having an OH-type anion exchange group, the basicity in the vicinity of the catalyst support increases, and hydrogen peroxide Decomposition characteristics or dissolved oxygen removal characteristics are enhanced. If the ion exchange capacity per volume in a water-wet state exceeds 1.8 mg equivalent / ml, the volume change of swelling and shrinkage of the monolith ion exchanger due to the change of the ion form tends to be too large. The ion exchange capacity per weight in the dry state of the fifth monolith ion exchanger is not particularly limited. However, since the ion exchange groups are uniformly introduced to the skeleton surface and the skeleton of the monolith ion exchanger, 3 ~ 5 mg equivalent / g.

  The fifth monolith and the fifth monolith ion exchanger have a thickness of 1 mm or more, and are distinguished from a membrane-like porous body. If the thickness is less than 1 mm, the ion exchange capacity per porous body is extremely low, which is not preferable. The thickness of the fifth monolith and the fifth monolith ion exchanger is preferably 3 to 1000 mm. The fifth monolith and the fifth monolith ion exchanger have high mechanical strength because the basic structure of the skeleton is a continuous pore structure.

<The manufacturing method of a 5th monolith and a 5th monolith ion exchanger>
The fifth monolith prepares a water-in-oil emulsion by stirring a mixture of an oil-soluble monomer that does not contain ion-exchange groups, a surfactant, and water, and then polymerizes the water-in-oil emulsion to form all pores. Step I to obtain a monolithic organic porous intermediate having a continuous macropore structure with a volume of 5 to 30 ml / g (hereinafter also referred to as monolith intermediate (5)), vinyl monomer, at least two or more in one molecule Obtained in Steps II and II of preparing a mixture comprising an organic solvent and a polymerization initiator that dissolves the vinyl monomer and the vinyl monomer and the crosslinking agent, but does not dissolve the polymer formed by polymerization of the vinyl monomer. A fifth monolith which is a composite monolith having a composite structure, wherein the mixture is allowed to stand for polymerization in the presence of the monolith intermediate (5) obtained in Step I. Obtaining step III, obtained by performing.

  What is necessary is just to perform I process which concerns on the manufacturing method of 5th monolith based on the method of Unexamined-Japanese-Patent No. 2002-306976.

  In the production of the monolith intermediate (5) of the step I according to the fifth monolith production method, examples of the oil-soluble monomer not containing an ion exchange group include a carboxylic acid group, a sulfonic acid group, a tertiary amino group, Examples thereof include an oleophilic monomer which does not contain an ion exchange group such as a quaternary ammonium group and has low solubility in water. Preferable examples of these monomers include styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, divinyl benzene, ethylene, propylene, isobutene, butadiene, ethylene glycol dimethacrylate, and the like. These monomers can be used singly or in combination of two or more. However, a crosslinkable monomer such as divinylbenzene or ethylene glycol dimethacrylate is selected as at least one component of the oil-soluble monomer, and the content thereof is 0.3 to 10 mol% in the total oil-soluble monomer, preferably 0.3 to When introducing an ion exchange group in a later step, it is preferable to set the amount to 5 mol% because the amount of ion exchange group can be quantitatively introduced.

  The surfactant used in Step I according to the fifth monolith production method can form a water-in-oil (W / O) emulsion when an oil-soluble monomer containing no ion exchange group and water are mixed. If it is a thing, there will be no restriction in particular, sorbitan monooleate, sorbitan monolaurate, sorbitan monopalmitate, sorbitan monostearate, sorbitan trioleate, polyoxyethylene nonyl phenyl ether, polyoxyethylene stearyl ether, polyoxyethylene sorbitan Nonionic surfactants such as monooleate; anionic surfactants such as potassium oleate, sodium dodecylbenzenesulfonate, dioctylsodium sulfosuccinate; cationic surfactants such as distearyldimethylammonium chloride; lauryl dimethyl It can be used an amphoteric surfactant such as Rubetain. These surfactants can be used singly or in combination of two or more. In addition, a water-in-oil emulsion refers to an emulsion in which an oil phase is a continuous phase and water droplets are dispersed therein. The amount of the surfactant added is not unclear because it varies greatly depending on the type of oil-soluble monomer and the size of the target emulsion particles (macropores), but the total amount of oil-soluble monomer and surfactant Can be selected within a range of about 2 to 70%.

  Moreover, in I process which concerns on the manufacturing method of a 5th monolith, you may use a polymerization initiator as needed in the case of water-in-oil type emulsion formation. As the polymerization initiator, a compound that generates radicals by heat or light irradiation is preferably used. The polymerization initiator may be water-soluble or oil-soluble. For example, 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2 , 2′-azobis (2-methylbutyronitrile), 2,2′-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2′-azobisisobutyrate, 4,4′-azobis ( 4-cyanovaleric acid), 1,1'-azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, ammonium persulfate, hydrogen peroxide-ferrous chloride, sodium persulfate- Examples include acidic sodium sulfite.

  As the mixing method when forming the water-in-oil emulsion by mixing an oil-soluble monomer that does not contain an ion exchange group, a surfactant, water, and a polymerization initiator in Step I according to the fifth monolith production method. There is no particular limitation, a method of mixing each component at once, an oil-soluble monomer, a surfactant, an oil-soluble component that is an oil-soluble polymerization initiator, and a water-soluble component that is water or a water-soluble polymerization initiator And the like can be separately dissolved, and then the respective components can be mixed. The mixing apparatus for forming the emulsion is not particularly limited, and a normal mixer, homogenizer, high-pressure homogenizer, or the like can be used, and an appropriate apparatus may be selected to obtain a desired emulsion particle size. Moreover, there is no restriction | limiting in particular also about mixing conditions, The stirring rotation speed and stirring time which can obtain the target emulsion particle size can be set arbitrarily.

  The monolith intermediate (5) obtained in step I according to the fifth method for producing a monolith has a continuous macropore structure. When this is allowed to coexist in the polymerization system, particles or the like are formed on the surface of the skeleton phase of the continuous macropore structure using the structure of the monolith intermediate (5) as a template, or particles on the surface of the skeleton phase of the co-continuous structure Or form. The monolith intermediate (5) is an organic polymer material having a crosslinked structure. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.3 to 10 mol%, preferably 0.3 to 5 mol% of crosslinked structural units with respect to all the structural units constituting the polymer material. Is preferred. When the cross-linking structural unit is less than 0.3 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, if it exceeds 10 mol%, the flexibility of the porous material is lost, and when an ion exchange group is introduced, it may be difficult to introduce the ion exchange group.

  In the step I relating to the fifth monolith production method, the kind of the polymer material of the monolith intermediate (5) is not particularly limited, and examples thereof include the same as the polymer material of the fifth monolith described above. Thereby, the same polymer is formed in the skeleton of the monolith intermediate (5), and the fifth monolith which is a monolith having a composite structure can be obtained.

  The total pore volume per weight in the dry state of the monolith intermediate (5) obtained in step I according to the fifth monolith production method is 5 to 30 ml / g, preferably 6 to 28 ml / g. . If the total pore volume of the monolith intermediate is too small, the total pore volume of the monolith obtained after polymerizing the vinyl monomer becomes too small, and the pressure loss during fluid permeation increases, which is not preferable. On the other hand, if the total pore volume of the monolith intermediate is too large, the structure of the monolith obtained after polymerizing the vinyl monomer tends to be non-uniform, which may cause structural collapse in some cases. In order to set the total pore volume of the monolith intermediate (5) in the above numerical range, the ratio (weight) of the monomer to water may be set to approximately 1: 5 to 1:35.

  In Step I according to the fifth method for producing a monolith, if the ratio of the monomer to water is approximately 1: 5 to 1:20, the total pore volume of the monolith intermediate (5) is 5 to 16 ml / g having a continuous macropore structure is obtained, and the monolith obtained through the step III is the 5-1 monolith. Further, if the blending ratio is approximately 1:20 to 1:35, the monolith intermediate (5) has a total pore volume of more than 16 ml / g and a continuous macropore structure of 30 ml / g or less. The monolith obtained through the step III becomes the 5-2 monolith.

  In addition, the monolith intermediate (5) obtained in Step I according to the fifth method for producing a monolith has an average diameter of 20 to 200 μm in the dry state of the opening (mesopore) that is the overlapping portion of the macropore and the macropore. When the average diameter of the opening in the dry state of the monolith intermediate is less than 20 μm, the opening diameter of the monolith and the monolith ion exchanger obtained after polymerizing the vinyl monomer is reduced, and the pressure loss during water passage is large. This is not preferable. On the other hand, when the average diameter of the opening in the dry state of the monolith intermediate exceeds 200 μm, the opening diameter of the monolith obtained after polymerizing the vinyl monomer and the monolith ion exchanger becomes too large. The contact with the monolith ion exchanger becomes insufficient, and as a result, the hydrogen peroxide decomposition characteristic or the dissolved oxygen removal characteristic is deteriorated. The monolith intermediate (5) is preferably of a uniform structure with a uniform macropore size and opening diameter, but is not limited to this, and the nonuniform macropore is larger than the uniform macropore size in the uniform structure. May be scattered.

  The II step relating to the fifth monolith production method comprises a vinyl monomer, a second crosslinking agent having at least two vinyl groups in one molecule, a vinyl monomer and a second crosslinking agent are dissolved, but the vinyl monomer is polymerized. This is a step of preparing a mixture comprising an organic solvent and a polymerization initiator that do not dissolve the polymer produced. In addition, there is no order of I process and II process, II process may be performed after I process, and I process may be performed after II process.

  The vinyl monomer used in Step II according to the fifth monolith production method is not particularly limited as long as it is a lipophilic vinyl monomer containing a polymerizable vinyl group in the molecule and having high solubility in an organic solvent. Absent. Specific examples of these vinyl monomers include aromatic vinyl monomers such as styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, vinyl biphenyl and vinyl naphthalene; α-olefins such as ethylene, propylene, 1-butene and isobutene; Diene monomers such as butadiene, isoprene and chloroprene; halogenated olefins such as vinyl chloride, vinyl bromide, vinylidene chloride and tetrafluoroethylene; nitrile monomers such as acrylonitrile and methacrylonitrile; vinyl such as vinyl acetate and vinyl propionate Esters: methyl acrylate, ethyl acrylate, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate, ethyl methacrylate, propyl methacrylate, butyl methacrylate, 2-methacrylic acid 2- Hexyl, cyclohexyl methacrylate, benzyl methacrylate, and (meth) acrylic monomer of glycidyl methacrylate. These monomers can be used alone or in combination of two or more. The vinyl monomer preferably used is an aromatic vinyl monomer such as styrene or vinyl benzyl chloride.

  The addition amount of the vinyl monomer used in Step II according to the fifth monolith production method is 3 to 50 times, preferably 4 to 40 times, by weight with respect to the monolith intermediate (5) to be coexisted during the polymerization. . If the amount of vinyl monomer added is less than 3 times that of the porous body, particles cannot be formed on the skeleton of the produced monolith, and when ion exchange groups are introduced, the volume per volume after introduction of ion exchange groups This is not preferable because the ion exchange capacity is reduced. On the other hand, if the amount of vinyl monomer added exceeds 50 times, the opening diameter becomes small, and the pressure loss during water passage becomes large, which is not preferable.

  As the crosslinking agent used in Step II according to the fifth monolith production method, a crosslinking agent containing at least two polymerizable vinyl groups in the molecule and having high solubility in an organic solvent is preferably used. Specific examples of the crosslinking agent include divinylbenzene, divinylnaphthalene, divinylbiphenyl, ethylene glycol dimethacrylate, trimethylolpropane triacrylate, butanediol diacrylate, and the like. These crosslinking agents can be used singly or in combination of two or more. Preferred cross-linking agents are aromatic polyvinyl compounds such as divinylbenzene, divinylnaphthalene and divinylbiphenyl because of their high mechanical strength and stability to hydrolysis. The amount of the crosslinking agent used is preferably 0.3 to 20 mol%, particularly preferably 0.3 to 10 mol%, based on the total amount of the vinyl monomer and the crosslinking agent. When the amount of the crosslinking agent used is less than 0.3 mol%, the mechanical strength of the monolith is insufficient, which is not preferable. On the other hand, if it exceeds 20 mol%, the brittleness of the monolith proceeds and the flexibility is lost, and when introducing an ion exchange group, the introduction amount of the ion exchange group may decrease, which is not preferable. .

  The organic solvent used in Step II of the fifth monolith production method is an organic solvent that dissolves the vinyl monomer and the crosslinking agent but does not dissolve the polymer formed by polymerization of the vinyl monomer, in other words, the vinyl monomer is polymerized. It is a poor solvent for the polymer produced. Since the organic solvent varies greatly depending on the type of vinyl monomer, it is difficult to list general specific examples. For example, when the vinyl monomer is styrene, the organic solvent includes methanol, ethanol, propanol, butanol, Alcohols such as hexanol, cyclohexanol, octanol, 2-ethylhexanol, decanol, dodecanol, propylene glycol, tetramethylene glycol; chain (poly) ethers such as diethyl ether, butyl cellosolve, polyethylene glycol, polypropylene glycol, polytetramethylene glycol Chain saturated hydrocarbons such as hexane, heptane, octane, isooctane, decane, dodecane, etc .; Ethyl acetate, isopropyl acetate, cellosolve acetate, ethyl propionate, etc. Ethers, and the like. Moreover, even if it is a good solvent of polystyrene like a dioxane, THF, and toluene, when it is used with the said poor solvent and the usage-amount is small, it can be used as an organic solvent. These organic solvents are preferably used so that the concentration of the vinyl monomer is 5 to 80% by weight. If the amount of the organic solvent used deviates from the above range and the vinyl monomer concentration is less than 5% by weight, the polymerization rate is lowered, which is not preferable. On the other hand, if the vinyl monomer concentration exceeds 80% by weight, the polymerization may run away, which is not preferable.

  As the polymerization initiator used in Step II according to the fifth method for producing a monolith, a compound that generates radicals by heat or light irradiation is suitably used. The polymerization initiator is preferably oil-soluble. Specific examples of the polymerization initiator include 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2,2′-azobis (2-methylbutyro). Nitrile), 2,2′-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2′-azobisisobutyrate, 4,4′-azobis (4-cyanovaleric acid), 1,1 ′ -Azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, tetramethylthiuram disulfide and the like. The amount of the polymerization initiator used varies greatly depending on the type of monomer, polymerization temperature, etc., but can be used in a range of about 0.01 to 5% with respect to the total amount of vinyl monomer and crosslinking agent.

  In step III according to the fifth monolith production method, the mixture obtained in step II is allowed to stand and polymerization is carried out in the presence of the monolith intermediate (5) obtained in step I. It is the process of obtaining. The monolith intermediate (5) used in the step III plays an extremely important role in creating the fifth monolith. As disclosed in JP-A-7-501140 and the like, when a vinyl monomer and a crosslinking agent are allowed to stand in a specific organic solvent in the absence of the monolith intermediate (5), a particle aggregation type monolith shape is obtained. An organic porous body is obtained. On the other hand, when the monolith intermediate (5) having a continuous macropore structure is present in the polymerization system as in the present invention, the structure of the composite monolith after the polymerization changes dramatically, not the particle aggregation structure. A fifth monolith having a specific skeletal structure is obtained. The internal volume of the reaction vessel is not particularly limited as long as it is large enough to allow the monolith intermediate (5) to be present in the reaction vessel, and when the monolith intermediate (5) is placed in the reaction vessel, the plan view In this case, the monolith may have a gap around the monolith or the monolith intermediate (5) may enter the reaction vessel without any gap. Of these, the fifth monolith after polymerization does not receive any pressure from the inner wall of the vessel and enters the reaction vessel without any gap, so that the fifth monolith is not distorted, and there is no waste of reaction raw materials and the like. Is. Even when the internal volume of the reaction vessel is large and a gap exists around the fifth monolith after polymerization, the vinyl monomer and the crosslinking agent are adsorbed and distributed on the monolith intermediate (5). In addition, a particle aggregate structure is not generated in a gap portion in the reaction vessel.

  In step III according to the fifth method for producing a monolith, the monolith intermediate (5) is placed in a state impregnated with the mixture (solution) in the reaction vessel. As described above, the blending ratio of the mixture obtained in Step II and the monolith intermediate (5) is 3 to 50 times, preferably 4 to 4 times, by weight with respect to the monolith intermediate (5). It is preferable to blend so as to be 40 times. As a result, a fifth monolith that is a composite monolith having a specific skeleton while having an appropriate opening diameter can be obtained. In the reaction vessel, the vinyl monomer and the cross-linking agent in the mixture are adsorbed and distributed on the skeleton of the monolith intermediate (5) that is allowed to stand, and polymerization proceeds in the skeleton of the monolith intermediate (5).

  In step III according to the fifth monolith production method, various polymerization conditions can be selected depending on the type of monomer and the type of initiator. For example, when 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), benzoyl peroxide, lauroyl peroxide, or the like is used as an initiator, an inert atmosphere What is necessary is just to heat-polymerize at 20-100 degreeC for 1 to 48 hours in the lower sealed container. By the heat polymerization, the vinyl monomer adsorbed and distributed on the skeleton of the monolith intermediate (5) and the crosslinking agent are polymerized in the skeleton to form the specific skeleton structure. After completion of the polymerization, the contents are taken out and extracted with a solvent such as acetone for the purpose of removing unreacted vinyl monomer and organic solvent to obtain a fifth monolith that is a composite monolith having a specific skeleton structure.

When the above-mentioned fifth monolith is produced, if the II step or the III step is performed under the conditions satisfying at least one of the following conditions (1) to (5), the characteristic structure of the fifth monolith is obtained. A monolith having a particle body or the like formed on the surface of the skeleton can be produced.
(1) The polymerization temperature in step III is a temperature that is at least 5 ° C. lower than the 10-hour half-life temperature of the polymerization initiator.
(2) The mole% of the crosslinking agent used in Step II is at least twice the mole% of the crosslinking agent used in Step I.
(3) The vinyl monomer used in step II is a vinyl monomer having a structure different from that of the oil-soluble monomer used in step I.
(4) The organic solvent used in step II is a polyether having a molecular weight of 200 or more.
(5) The concentration of the vinyl monomer used in Step II is 30% by weight or less in the mixture of Step II.

(Description of (1) above)
The 10-hour half temperature is a characteristic value of the polymerization initiator, and if the polymerization initiator to be used is determined, the 10-hour half temperature can be known. Moreover, if there exists desired 10-hour half temperature, the polymerization initiator applicable to it can be selected. In step III, the polymerization rate is lowered by lowering the polymerization temperature, and particles and the like can be formed on the surface of the skeleton phase. The reason for this is that the monomer concentration drop inside the skeleton phase of the monolith intermediate becomes gradual, and the monomer distribution rate from the liquid phase part to the monolith intermediate decreases, so the surplus monomer is on the surface of the skeleton layer of the monolith intermediate. It is thought that it was concentrated in the vicinity and polymerized in situ.

  In Step III according to the fifth monolith production method, a preferable polymerization temperature is a temperature that is at least 10 ° C. lower than the 10-hour half-life temperature of the polymerization initiator used. Although the lower limit of the polymerization temperature is not particularly limited, the polymerization rate decreases as the temperature decreases, and the polymerization time becomes unacceptably long. Therefore, the polymerization temperature is 5 to 20 ° C. with respect to the 10-hour half temperature. It is preferable to set to a low range.

(Explanation of (2) above)
When the mol% of the cross-linking agent used in the step II according to the fifth monolith production method is set to be 2 times or more of the mol% of the cross-linking agent used in the I step, a monolith having a composite structure is obtained. The reason for this is that the compatibility between the monolith intermediate and the polymer produced by impregnation polymerization is reduced and phase separation proceeds, so the polymer produced by impregnation polymerization is excluded in the vicinity of the surface of the skeleton phase of the monolith intermediate, It is considered that irregularities such as particles are formed on the surface. In addition, mol% of a crosslinking agent is a crosslinking density mol%, Comprising: The amount of crosslinking agents (mol%) with respect to the total amount of a vinyl monomer and a crosslinking agent is said.

  The upper limit of the crosslinker mol% used in Step II of the fifth monolith production method is not particularly limited, but when the crosslinker mol% is extremely large, cracks occur in the monolith after polymerization, and the monolith becomes brittle. Thus, flexibility is lost, and when an ion exchange group is introduced, the amount of ion exchange group introduced may be reduced, which is not preferable. The preferred multiple of the crosslinker mol% is 2 to 10 times. On the other hand, even if the crosslinker mol% used in Step I is set to be twice or more the crosslinker mol% used in Step II, the formation of particles on the surface of the skeleton phase does not occur, and the fifth monolith Was not obtained.

(Description of (3) above)
If the vinyl monomer used in step II according to the fifth monolith production method is a vinyl monomer having a structure different from that of the oil-soluble monomer used in step I, the fifth monolith is obtained. For example, if the structures of vinyl monomers are slightly different, such as styrene and vinyl benzyl chloride, a composite monolith having particles or the like formed on the surface of the skeleton phase is generated. In general, two types of homopolymers obtained from two types of monomers that are slightly different in structure are not compatible with each other. Therefore, when a monomer having a structure different from that used for forming the monolith intermediate used in Step I is used in Step II and polymerization is performed in Step III, the monomer used in Step II is uniformly distributed to the monolith intermediate. Although impregnation occurs, when polymerization proceeds and a polymer is produced, the produced polymer is incompatible with the monolith intermediate, so phase separation proceeds, and the produced polymer is near the surface of the skeleton phase of the monolith intermediate. It is considered that irregularities such as particles are formed on the surface of the skeleton phase.

(Explanation of (4) above)
A 5th monolith is obtained when the organic solvent used by II process concerning the manufacturing method of a 5th monolith is a polyether with a molecular weight of 200 or more. Polyethers have a relatively high affinity with monolith intermediates, especially low molecular weight cyclic polyethers are good solvents for polystyrene, and low molecular weight chain polyethers are not good solvents but have considerable affinity. . However, as the molecular weight of the polyether increases, the affinity with the monolith intermediate dramatically decreases and shows little affinity with the monolith intermediate. When such a solvent having poor affinity is used as the organic solvent, diffusion of the monomer into the skeleton of the monolith intermediate is inhibited, and as a result, the monomer is polymerized only near the surface of the skeleton of the monolith intermediate. It is considered that particles and the like are formed on the phase surface and irregularities are formed on the skeleton surface.

  The upper limit of the molecular weight of the polyether used in Step II according to the fifth monolith production method is not particularly limited as long as it is 200 or more. However, if the molecular weight is too high, the viscosity of the mixture prepared in Step II is high. Therefore, it is not preferable because it is difficult to impregnate the monolith intermediate. The molecular weight of the preferred polyether is 200 to 100,000, particularly preferably 200 to 10,000. The terminal structure of the polyether may be an unmodified hydroxyl group, etherified with an alkyl group such as a methyl group or an ethyl group, or esterified with acetic acid, oleic acid, lauric acid, stearic acid, or the like. It may be made.

(Description of (5) above)
The fifth monolith is obtained when the concentration of the vinyl monomer used in step II according to the fifth monolith production method is 30% by weight or less in the mixture in step II. By reducing the monomer concentration in the step II, the polymerization rate is reduced, and for the same reason as the above (1), particles and the like can be formed on the surface of the skeleton phase, and irregularities can be formed on the surface of the skeleton phase. . Although the lower limit of the monomer concentration is not particularly limited, the polymerization rate decreases as the monomer concentration decreases and the polymerization time becomes unacceptably long, so the monomer concentration may be set to 10 to 30% by weight. preferable.

  As a preferable structure of the fifth monolith thus obtained, bubble-shaped macropores overlap each other, and the overlapping portion is a continuous macropore structure (“5-1th” in which openings have an average diameter of 10 to 120 μm in a dry state. Monolith of the three-dimensional continuous skeleton having an average thickness of 0.8 to 40 μm in a dry state, and three-dimensional continuous pores having a diameter in the dry state of 8 to 80 μm between the skeletons. And a co-continuous structure (“5-2 monolith”).

  When the fifth monolith is the 5-1 monolith, the 5-1 monolith has bubble-like macropores that overlap each other, and the overlapping portion has an average diameter of 10 to 120 μm, preferably 20 to 120 μm, especially in a dry state. Preferably, it is a continuous macropore structure which becomes an opening (mesopore) of 25 to 120 μm, and the inside of bubbles formed by the macropore and the opening (mesopore) is a flow path. The continuous macropore structure is preferably a uniform structure having the same macropore size and aperture diameter, but is not limited to this, and the uniform structure is dotted with nonuniform macropores larger than the size of the uniform macropore. You may do. If the average diameter of the opening in the dry state of the 5-1 monolith is less than 10 μm, it is not preferable because the pressure loss at the time of passing water becomes large. If it exceeds, the contact between the water to be treated and the monolith ion exchanger and the supported platinum group metal particles becomes insufficient, and as a result, the hydrogen peroxide decomposition characteristics or the dissolved oxygen removal characteristics deteriorate, which is not preferable.

  In the case of the 5-2 monolith, the 5-2 monolith has a three-dimensional continuous skeleton having an average thickness of 0.8 to 40 μm in a dry state, and an average diameter in a dry state between the skeletons. Is a co-continuous structure having three-dimensionally continuous pores of 8 to 80 μm. If the average diameter in the dry state of the three-dimensionally continuous pores of the 5-2 monolith is less than 8 μm, it is not preferable because the pressure loss during water flow increases, and if it exceeds 80 μm Further, the contact between the water to be treated and the monolith or monolith ion exchanger and the supported platinum group metal particles becomes insufficient, and as a result, the hydrogen peroxide decomposition characteristics or the dissolved oxygen removal characteristics deteriorate, which is not preferable. Further, when the average thickness in the dry state of the skeleton of the 5-2 monolith is less than 0.8 μm, when ion exchange groups are introduced, the ion exchange capacity per volume of the monolith ion exchanger decreases. In addition to the disadvantages, the mechanical strength is lowered, and the monolith or monolith ion exchanger is greatly deformed particularly when water is passed at a high flow rate. On the other hand, if the average thickness of the skeleton in a dry state exceeds 80 μm, the pressure loss during water passage increases, which is not preferable.

  The fifth monolith ion exchanger is obtained by performing an IV step for introducing an ion exchange group into the fifth monolith obtained in the step III.

  The method for introducing ion exchange groups into the fifth monolith is the same as the method for introducing ion exchange groups into the first monolith.

<Description of Sixth Monolith and Sixth Monolith Ion Exchanger>
In the platinum group metal-supported catalyst of the present invention, the sixth monolith and the sixth monolith ion exchanger serving as the carrier for the platinum group metal particles overlap with each other in the form of bubble-like macropores, and the overlapping portion has an average diameter in a wet state. A continuous macropore structure having an opening of 20 to 300 μm, and an organic porous body having a porous structure in the surface layer of the skeleton of the continuous macropore structure. The sixth monolith ion exchanger has an ion exchange group, an ion exchange capacity per volume in a water-wet state is 0.4 mg equivalent / ml or more, and the ion exchange group is an organic porous material. It is a monolithic ion exchanger that is uniformly distributed in the ion exchanger.

  The sixth monolith and the sixth monolith ion exchanger will be described with reference to FIG. 10, which is a schematic diagram showing the basic structure of the sixth monolith and the sixth monolith ion exchanger. In FIG. 10, the square on the right side is an enlarged schematic view of the wall portion (skeleton portion) A of the sixth monolith (or monolith ion exchanger). The sixth monolith (or monolith ion exchanger) 30 has a continuous macropore structure in which bubble-like macropores 31 overlap each other, and the overlapping portion becomes a common opening (mesopore) 32, and the average diameter of the openings 32 is in a wet state. 20 to 300 μm, preferably 20 to 200 μm, particularly 20 to 150 μm, and the inside of the open cell formed by the macropore 31 and the opening 32 becomes a flow path. The continuous macropore structure is preferably a uniform structure having the same macropore size and aperture diameter, but is not limited to this, and the uniform structure is dotted with nonuniform macropores larger than the size of the uniform macropore. You may do. If the average diameter of the sixth monolith or the sixth monolith ion exchanger in the water-wet state (mesopore) is less than 20 μm, it is not preferable because the pressure loss at the time of passing water becomes large. When the average diameter of the openings (mesopores) in the wet state exceeds 300 μm, the contact between the water to be treated and the monolith or monolith ion exchanger becomes insufficient. As a result, hydrogen peroxide decomposition characteristics or dissolved oxygen removal characteristics are not obtained. Since it falls, it is not preferable.

  The average diameter of the opening of the sixth monolith in the dry state, the average diameter of the opening of the sixth monolith ion exchanger in the dry state, and the dry state obtained in step I relating to the sixth monolith production method described below The average diameter of the opening of the monolith intermediate (6) is the maximum value of the pore distribution curve obtained by the mercury intrusion method. In addition, the average diameter of the openings of the sixth monolith or the sixth monolith ion exchanger in the wet state of water is the average diameter of the openings of the sixth monolith or the sixth monolith ion exchanger in the dry state. It is a value calculated by multiplication. Specifically, the diameter of the sixth monolith (or monolith ion exchanger) in the water wet state is x1 (mm), and the sixth monolith (or monolith ion exchanger) in the water wet state is dried, The diameter of the obtained sixth monolith (or monolith ion exchanger) in the dry state is y1 (mm), and the sixth monolith (or monolith ion exchanger) in the dry state is measured by a mercury intrusion method. Assuming that the average diameter of the opening is z1 (μm), the average diameter (μm) of the sixth monolith (or monolith ion exchanger) in the water wet state is expressed by the following formula: (Or average diameter (μm) = z1 × (x1 / y1)) of openings of (or monolith ion exchanger) ”. Further, the average diameter of the opening of the sixth monolith in the dry state before the introduction of the ion exchange group, and the water wet state relative to the sixth monolith in the dry state when the ion exchange group is introduced into the sixth monolith in the dry state. When the swelling ratio of the sixth monolith ion exchanger is known, the average diameter of the sixth monolith ion exchanger in the water-wet state is obtained by multiplying the average diameter of the opening of the sixth monolith in the dry state by the swelling ratio. The diameter can also be calculated.

  The sixth monolith (or monolith ion exchanger) 30 has a porous structure in the surface layer portion of the skeleton, but the proportion of the surface layer portion in the skeleton is small, and the porous structure is discontinuous like a “nest”. Since the pores are the majority, the average diameter of mesopores can be determined by mercury porosimetry.

  In the sixth monolith (or monolith ion exchanger) 30, the skeleton portion 36 of the continuous macropore structure includes an inner layer portion 33 and a surface layer portion 34, and the surface layer portion 34 has a porous structure. In other words, the porous structure has a structure in which the surface layer portion 34 has innumerable pores 37 with a diameter of 0.1 to 30 μm, particularly 0.1 to 15 μm in a water-wet state, and the surface layer portion has a structure similar to a so-called honeycomb. It is. The large number of pores 37 may be independent from each other or may be adjacent to each other. The thickness of the surface layer portion 34 in a wet state is approximately 1 to 45 μm. In FIG. 10, reference numeral 35 denotes a gas phase (bubble) part. The porous structure of the skeleton part 36 can be confirmed by an SEM (secondary electron image by a scanning electron microscope) image of a surface obtained by cutting the sixth monolith (or monolith ion exchanger) (dry body). FIG. 11 shows an SEM photograph of an example of the sixth monolith, in which a large number of pores are formed in the surface layer portion of the skeleton portion. The sixth monolith (or monolith ion exchanger) 30 is one in which the pores 37 constituting the porous structure are not observed from the outside (hereinafter referred to as “integrated sixth monolith or sixth monolith ion exchanger”). ) Or a structure in which pores 37 forming a porous structure are observed from the outside on the end face such as a skeleton cut surface (hereinafter also referred to as “cut type sixth monolith or sixth monolith ion exchanger”). .). The monolithic sixth monolith or the sixth monolith ion exchanger is removed from the reaction vessel and is not cut, and the cut sixth monolith or the sixth monolith ion exchanger is cut with a blade or the like. Dice shape. If the platinum group metal-supported catalyst of the present invention, in which a platinum group metal is supported on the sixth monolith or the sixth monolith ion exchanger, is used as a catalyst, the penetration of the liquid into the surface layer of the porous structure is fast and the contact efficiency is improved. The catalyst activity increases.

  The pore diameter of the surface layer portion of the continuous macropore structure in the wet state is determined by performing SEM observation of the sixth monolith in the dry state or the sixth monolith ion exchanger at least three times, and the fine diameter in the obtained image. It is a value calculated by measuring the pore diameter and multiplying the average value by the swelling rate. Specifically, the diameter of the sixth monolith (or monolith ion exchanger) in the water wet state is x2 (mm), and the sixth monolith (or monolith ion exchanger) in the water wet state is dried, The diameter of the obtained sixth monolith (or monolith ion exchanger) in the dry state is y2 (mm), and SEM observation of the sixth monolith (or monolith ion exchanger) in the dry state is performed at least three times, When the pore diameter in the obtained image was measured and the average value was z2 (μm), the surface layer portion of the continuous structure of the sixth monolith (or monolith ion exchanger) in the water wet state was used. The pore diameter (μm) is the pore diameter (μm) of the surface layer portion of the continuous macropore structure of the following formula “sixth monolith (or monolith ion exchanger) in a water wet state = z2 × (x2 / y2) Is calculated. Further, the pore diameter of the surface layer portion of the sixth monolith in the dry state before the introduction of the ion exchange group, and water wetting with respect to the sixth monolith in the dry state when the ion exchange group is introduced into the sixth monolith in the dry state When the swelling ratio of the sixth monolith ion exchanger in the state is known, the sixth monolith ion exchanger in the water wet state is obtained by multiplying the pore diameter of the surface layer portion of the sixth monolith in the dry state by the swelling ratio. It is also possible to calculate the pore diameter of the surface layer portion. Note that the thickness of the surface layer portion of the sixth monolith or the sixth monolith ion exchanger can also be calculated in the same manner.

Note that the cut-type sixth monolith or the sixth monolith anion exchanger has a remarkably large specific surface area because the porous structure of the surface portion of the skeleton portion appears on the surface, and in most cases, the sixth monolith or the sixth monolith The specific surface area measured by drying the monolithic ion exchanger was 20 to 70 m ² / g. Since the cut-type sixth monolith or the sixth monolith ion exchanger has a large specific surface area, when the platinum group metal-supported catalyst of the present invention supporting platinum group metal particles is used as a catalyst, Since the contact area is large and fluid can be smoothly circulated, excellent catalytic performance can be exhibited. In the present invention, the specific surface areas of the sixth monolith and the sixth monolith ion exchanger are values obtained by measuring the dried body by a mercury intrusion method.

  The sixth monolith and the sixth monolith ion exchanger can increase the aperture diameter, thicken the skeleton of the continuous macropore structure (thicken the skeleton wall), and have a porous structure in the surface layer. Therefore, the catalyst activity can be dramatically increased while keeping the pressure loss during permeation low.

  Further, the total pore volume per weight in the dry state of the sixth monolith and the sixth monolith ion exchanger is 0.5 to 5 ml / g, preferably 0.8 to 4 ml / g. If the total pore volume is less than 0.5 ml / g, the amount of permeated liquid and the amount of permeated gas per unit cross-sectional area will be reduced, and the processing capacity will be reduced. On the other hand, if the total pore volume exceeds 5 ml / g, the catalytic activity is lowered, which is not preferable.

  In addition, the pressure loss at the time of making water permeate | transmit the 6th monolith and the 6th monolith ion exchanger is the water flow velocity (LV) to the column packed with 1 m of the 6th monolith or the 6th monolith ion exchanger. ) In terms of pressure loss when water is passed at 1 m / h (hereinafter referred to as “differential pressure coefficient”), a range of 0.005 to 0.1 MPa / m · LV, particularly 0.005 to 0.05 MPa. / M · LV is preferred.

  The ion exchange group introduced into the sixth monolith ion exchanger is the same as the ion exchange group introduced into the first monolith ion exchanger.

  In the sixth monolith ion exchanger, the introduced ion exchange groups are uniformly distributed not only on the surface of the organic porous body but also within the skeleton of the organic porous body. Further, when the ion exchange group is uniformly distributed not only on the surface of the sixth monolith ion exchanger but also inside the skeleton, the physical and chemical properties of the surface and the inside can be made uniform, so that the swelling And durability against shrinkage is improved.

  The sixth monolith ion exchanger has an ion exchange capacity per volume in a water wet state of 0.4 mg equivalent / ml or more, preferably 0.4 to 1.8 mg equivalent / ml. If the ion exchange capacity per volume of the monolith ion exchanger is within the above range, in the case of a monolith ion exchanger having an OH-type anion exchange group, the basicity in the vicinity of the catalyst support is high, and hydrogen peroxide decomposition characteristics Or the dissolved oxygen removal property becomes high. If the ion exchange capacity per volume in a water-wet state exceeds 1.8 mg equivalent / ml, the volume change of swelling and shrinkage of the monolith ion exchanger due to the change of the ion form tends to be too large. In addition, the ion exchange capacity per weight in the dry state of the sixth monolith ion exchanger is not particularly limited. However, since the ion exchange groups are uniformly introduced to the skeleton surface and inside the skeleton of the monolith ion exchanger, 3 ˜5 mg equivalent / g (dry body).

  The sixth monolith and the sixth monolith ion exchanger have a thickness of 1 mm or more, and are distinguished from a membrane-like porous body. The thickness of the sixth monolith and the sixth monolith ion exchanger is preferably 3 to 1000 mm. The sixth monolith and the sixth monolith ion exchanger have high mechanical strength because the basic structure of the skeleton is a continuous macropore structure.

  In the sixth monolith and the sixth monolith ion exchanger, the material constituting the skeleton of the continuous macropore structure, that is, the skeleton part 41 of the inner layer part 33 and the surface layer part 34 is an organic polymer material having a crosslinked structure.

  In the sixth monolith and the sixth monolith ion exchanger, the crosslinking density of the polymer material is not particularly limited, but is 0.1 to 10 mol%, preferably 0, based on all the structural units constituting the polymer material. It is preferable that 2 to 5 mol% of cross-linked structural units are contained. If the cross-linking structural unit is less than 0.1 mol%, the mechanical strength is insufficient, which is not preferable. On the other hand, if it exceeds 10 mol%, introduction of a porous structure into the skeleton of the continuous macropore structure is not recognized. It is not preferable. The type of the polymer material is not particularly limited, and examples thereof include aromatic vinyl polymers such as polystyrene, poly (α-methylstyrene), polyvinyl toluene, polyvinyl benzyl chloride, polyvinyl biphenyl, and polyvinyl naphthalene; polyolefins such as polyethylene and polypropylene; Poly (halogenated polyolefin) such as vinyl chloride and polytetrafluoroethylene; Nitrile-based polymer such as polyacrylonitrile; Cross-linking weight of (meth) acrylic polymer such as polymethyl methacrylate, polyglycidyl methacrylate, and polyethyl acrylate Coalescence is mentioned. The polymer may be a polymer obtained by copolymerizing a single vinyl monomer and a crosslinking agent, a polymer obtained by polymerizing a plurality of vinyl monomers and a crosslinking agent, or a blend of two or more types of polymers. It may be what was done. Among these organic polymer materials, the cross-linking weight of the aromatic vinyl polymer is easy due to the ease of forming a continuous macropore structure, the ease of introducing ion exchange groups and the high mechanical strength, and the high stability to acids and alkalis. A styrene-divinylbenzene copolymer and a vinylbenzyl chloride-divinylbenzene copolymer are particularly preferable materials.

<Method for Producing Sixth Monolith and Sixth Monolith Ion Exchanger>
The sixth monolith prepares a water-in-oil emulsion by stirring a mixture of oil-soluble monomer, surfactant and water that does not contain ion exchange groups, and then polymerizes the water-in-oil emulsion to form a total pore. Step I for obtaining a monolithic organic porous intermediate (hereinafter also referred to as monolith intermediate (6)) having a continuous macropore structure with a volume of 5 to 16 ml / g, at least two or more vinyl monomers in one molecule A mixture of a vinyl group-containing crosslinking agent, an aliphatic alcohol having 3 to 9 carbon atoms and a polymerization initiator, wherein the vinyl monomer concentration in the vinyl monomer, crosslinking agent and aliphatic alcohol mixture (wt% ) Of 56 to 80%, or the vinyl monomer concentration is 40% or more and less than 56%, and the bridge for the total amount of vinyl monomer and crosslinking agent Step II in which the amount of the agent is 0.1 to 1 mol%, the mixture obtained in Step II is left standing, and polymerization is performed in the presence of the monolith intermediate (6) obtained in Step I, It is obtained by carrying out step III to obtain a sixth monolith.

  In the sixth method for producing a monolith, the step I may be performed in accordance with the method described in JP-A-2002-306976.

  In the production of the monolith intermediate (6) in the step I according to the sixth monolith production method, examples of the oil-soluble monomer containing no ion exchange group include a carboxylic acid group, an iminodiacetic acid group, a sulfonic acid group, phosphorus Examples include cation exchange groups such as acid groups and phosphate ester groups and anion exchange groups such as tertiary amino groups and quaternary ammonium groups, and low water solubility and lipophilic monomers. Preferable examples of these monomers include styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, divinyl benzene, ethylene, propylene, isobutene, butadiene, ethylene glycol dimethacrylate, and the like. These monomers can be used singly or in combination of two or more. However, a crosslinkable monomer (crosslinking agent) such as divinylbenzene or ethylene glycol dimethacrylate is selected as at least one component of the oil-soluble monomer, and its content is 0.1 to 10 mol% in the total oil-soluble monomer, preferably The amount is preferably 0.2 to 5 mol% because the amount of ion-exchange groups can be quantitatively introduced in the subsequent step.

  The surfactant used in step I according to the sixth method for producing a monolith can form a water-in-oil (W / O) emulsion when an oil-soluble monomer containing no ion exchange group and water are mixed. If it is a thing, there will be no restriction in particular, sorbitan monooleate, sorbitan monolaurate, sorbitan monopalmitate, sorbitan monostearate, sorbitan trioleate, polyoxyethylene nonyl phenyl ether, polyoxyethylene stearyl ether, polyoxyethylene sorbitan Nonionic surfactants such as monooleate; anionic surfactants such as potassium oleate, sodium dodecylbenzenesulfonate, dioctylsodium sulfosuccinate; cationic surfactants such as distearyldimethylammonium chloride; lauryl dimethyl It can be used an amphoteric surfactant such as Rubetain. These surfactants can be used singly or in combination of two or more. In addition, a water-in-oil emulsion refers to an emulsion in which an oil phase is a continuous phase and water droplets are dispersed therein. The amount of the surfactant added is not unclear because it varies greatly depending on the type of oil-soluble monomer and the size of the target emulsion particles (macropores), but the total amount of oil-soluble monomer and surfactant Can be selected within a range of about 2 to 70%.

  Moreover, in I process which concerns on the manufacturing method of a 6th monolith, you may use a polymerization initiator as needed in the case of water-in-oil type emulsion formation. As the polymerization initiator, a compound that generates radicals by heat or light irradiation is preferably used. The polymerization initiator may be water-soluble or oil-soluble. For example, 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2 , 2′-azobis (2-methylbutyronitrile), 2,2′-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2′-azobisisobutyrate, 4,4′-azobis ( 4-cyanovaleric acid), 1,1'-azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, potassium persulfate, ammonium persulfate, hydrogen peroxide-ferrous chloride, sodium persulfate- Examples include acidic sodium sulfite.

  In the step I relating to the sixth method for producing a monolith, as a mixing method when an oil-soluble monomer not containing an ion exchange group, a surfactant, water and a polymerization initiator are mixed to form a water-in-oil emulsion. There is no particular limitation, a method of mixing each component at once, an oil-soluble monomer, a surfactant, an oil-soluble component that is an oil-soluble polymerization initiator, and a water-soluble component that is water or a water-soluble polymerization initiator And the like can be separately dissolved, and then the respective components can be mixed. The mixing apparatus for forming the emulsion is not particularly limited, and a normal mixer, homogenizer, high-pressure homogenizer, or the like can be used, and an appropriate apparatus may be selected to obtain a desired emulsion particle size. Moreover, there is no restriction | limiting in particular about mixing conditions, The stirring rotation speed and stirring time which can obtain the target emulsion particle size can be set arbitrarily.

  The monolith intermediate (6) obtained in step I according to the sixth method for producing a monolith has a continuous macropore structure. When this coexists in a polymerization system, a surface layer portion of a porous structure is formed on the surface of the skeleton of the monolith intermediate (6) using the structure of the monolith intermediate (6) as a template. A porous body structure is formed. The monolith intermediate (6) is an organic polymer material having a crosslinked structure. Although the crosslinking density of the polymer material is not particularly limited, it contains 0.1 to 10 mol%, preferably 0.2 to 5 mol% of crosslinked structural units with respect to all the structural units constituting the polymer material. Is preferred. When the cross-linking structural unit is less than 0.1 mol%, the mechanical strength is insufficient, which is not preferable. In particular, when the total pore volume is as large as 10 to 16 ml / g, in order to maintain a continuous macropore structure, it is preferable to contain 0.2 mol% or more of cross-linked structural units. On the other hand, when it exceeds 10 mol%, it becomes difficult to introduce a porous structure into the surface layer portion of the skeleton portion of the continuous macropore structure.

  In the step I relating to the sixth monolith production method, the kind of the polymer material of the monolith intermediate (6) is not particularly limited, and the polymer material of the sixth monolith and the sixth monolith ion exchanger described above The same can be mentioned. Thereby, the same polymer is formed in the skeleton of the monolith intermediate (6), and a sixth monolith that is a monolith having a thick skeleton structure having a porous structure in the surface layer portion can be obtained.

  The total pore volume per weight in the dry state of the monolith intermediate (6) obtained in Step I according to the sixth method for producing a monolith is 5 to 16 ml / g, preferably 6 to 16 ml / g. . If the total pore volume of the monolith intermediate is too small, the total pore volume of the monolith obtained after polymerizing the vinyl monomer becomes too small, and the pressure loss during permeation of the water to be treated becomes large. On the other hand, if the total pore volume of the monolith intermediate is too large, the structure of the monolith obtained after polymerizing the vinyl monomer deviates from the continuous macropore structure, which is not preferable. In order to set the total pore volume of the monolith intermediate (6) within the above numerical range, the ratio of monomer to water (weight) may be set to approximately 1: 5 to 1:16.

  In addition, the monolith intermediate (6) obtained in the step I according to the sixth method for producing a monolith has an average diameter of 15 to 200 μm in the dry state of openings (mesopores) that are overlapping portions of macropores and macropores. If the average diameter of the opening in the dry state of the monolith intermediate is less than 15 μm, it is preferable because the opening diameter of the monolith obtained after polymerizing the vinyl monomer becomes small and the pressure loss during water passage increases. Absent. On the other hand, when the average diameter of the opening in the dry state of the monolith intermediate exceeds 200 μm, the opening diameter of the monolith obtained after polymerizing the vinyl monomer becomes too large, and the water to be treated and the monolith or monolith ion exchanger As a result, the hydrogen peroxide decomposition characteristic or the dissolved oxygen removal characteristic deteriorates, which is not preferable. Monolith intermediates preferably have a uniform structure with uniform macropore size and aperture diameter, but are not limited to this, and the uniform structure is dotted with nonuniform macropores larger than the size of the uniform macropore. You may do.

  Step II relating to the sixth monolith production method comprises a mixture comprising a vinyl monomer, a second crosslinking agent having at least two or more vinyl groups in one molecule, an aliphatic alcohol having 3 to 9 carbon atoms, and a polymerization initiator. The vinyl monomer concentration (wt%) in the vinyl monomer, second cross-linking agent and aliphatic alcohol mixture is 56 to 80%, or the vinyl monomer concentration is 40% or more and less than 56%. And the amount of the second crosslinking agent relative to the total amount of the vinyl monomer and the second crosslinking agent is 0.1 to 1 mol%. In addition, there is no order of I process and II process, II process may be performed after I process, and I process may be performed after II process.

  The vinyl monomer used in Step II according to the sixth monolith production method is not particularly limited as long as it is a lipophilic vinyl monomer containing a polymerizable vinyl group in the molecule and having high solubility in an organic solvent. Absent. Specific examples of these vinyl monomers include aromatic vinyl monomers such as styrene, α-methylstyrene, vinyl toluene, vinyl benzyl chloride, vinyl biphenyl and vinyl naphthalene; α-olefins such as ethylene, propylene, 1-butene and isobutene; Diene monomers such as butadiene, isoprene and chloroprene; halogenated olefins such as vinyl chloride, vinyl bromide, vinylidene chloride and tetrafluoroethylene; nitrile monomers such as acrylonitrile and methacrylonitrile; vinyl such as vinyl acetate and vinyl propionate Esters: methyl acrylate, ethyl acrylate, butyl acrylate, 2-ethylhexyl acrylate, methyl methacrylate, ethyl methacrylate, propyl methacrylate, butyl methacrylate, 2-methacrylic acid 2- Hexyl, cyclohexyl methacrylate, benzyl methacrylate, and (meth) acrylic monomer of glycidyl methacrylate. These monomers can be used alone or in combination of two or more. The vinyl monomer preferably used is an aromatic vinyl monomer such as styrene or vinyl benzyl chloride.

  In the II step related to the sixth monolith production method, when the vinyl monomer concentration (wt%) in the mixture of the vinyl monomer, the second crosslinking agent and the aliphatic alcohol is 56 to 80%, the vinyl monomer and the second crosslinking agent The amount of the second crosslinking agent with respect to the total amount is preferably 0.1 to 5 mol%, more preferably 0.3 to 4 mol%. On the other hand, when the vinyl monomer concentration in the vinyl monomer, second crosslinking agent and aliphatic alcohol mixture is 40% or more and less than 56%, the amount of the second crosslinking agent relative to the total amount of the vinyl monomer and the second crosslinking agent is 0. 0.1 to 1 mol%, preferably 0.2 to 1 mol%. When the vinyl monomer concentration deviates from the above range, introduction of a porous structure into the skeleton is not recognized. On the other hand, if the vinyl monomer concentration exceeds 80%, it is difficult to remove the heat of polymerization and it is difficult to control the polymerization reaction.

  In step II according to the sixth method for producing a monolith, the amount of vinyl monomer added is 3 to 70 times, preferably 4 to 50 times, by weight with respect to the monolith intermediate (6) to be coexisted during polymerization. If the amount of vinyl monomer added is less than 3 times that of the monolith intermediate, it is not preferable because it becomes difficult to introduce a porous structure into the skeleton. On the other hand, when the added amount of vinyl monomer exceeds 70 times, the opening diameter becomes small, and the pressure loss during water passage becomes large, which is not preferable.

  The second cross-linking agent used in Step II according to the sixth method for producing a monolith preferably contains at least two polymerizable vinyl groups in the molecule and has high solubility in an organic solvent. . Specific examples of the second crosslinking agent include divinylbenzene, divinylnaphthalene, divinylbiphenyl, ethylene glycol dimethacrylate, trimethylolpropane triacrylate, butanediol diacrylate, and the like. These 2nd crosslinking agents can be used individually by 1 type or in combination of 2 or more types. A preferred second crosslinking agent is an aromatic polyvinyl compound such as divinylbenzene, divinylnaphthalene, and divinylbiphenyl because of its high mechanical strength and stability to hydrolysis. The amount of the second crosslinking agent used varies depending on the vinyl monomer concentration (% by weight) in the vinyl monomer, the second crosslinking agent, and the aliphatic alcohol mixture, but it is 0.00% relative to the total amount of the vinyl monomer and the second crosslinking agent. It is preferable that it is 1-5 mol%, especially 0.2-5 mol%. If the amount of the second crosslinking agent used is less than 0.1 mol%, the mechanical strength of the monolith is insufficient, which is not preferable. On the other hand, if it exceeds 5 mol%, it is difficult to introduce a porous structure into the skeleton, which is not preferable. The amount of the second cross-linking agent used is preferably used so as to be approximately equal to the cross-linking density of the monolith intermediate coexisting during the polymerization of the vinyl monomer / second cross-linking agent. If the amounts used of both are too large, the crosslink density distribution will be biased in the produced monolith, and when ion exchange groups are introduced, cracks are likely to occur during the ion exchange group introduction reaction.

  The solvent used in step II according to the sixth method for producing a monolith is an aliphatic alcohol having 3 to 9 carbon atoms. Specific examples of the aliphatic alcohol include 1-propanol, 2-propanol, 1-butanol, isobutanol, sec-butanol, t-butanol, 1-pentanol, 1-hexanol, cyclohexanol, 1-octanol, 2 -Ethylhexanol, ethylene glycol, propylene glycol, tetramethylene glycol, glycerin, cellosolve, methyl cellosolve, butyl cellosolve and the like. Moreover, even if it is a solvent other than the said aliphatic alcohol, when the usage-amount is small, it can be added and used for the said aliphatic alcohol. It is preferable to use these aliphatic alcohols so that the vinyl monomer concentration is 40 to 80% by weight. If the amount of aliphatic alcohol used deviates from the above range and the vinyl monomer concentration is less than 40%, it is not preferable because it becomes difficult to introduce a porous structure into the skeleton. On the other hand, if the vinyl monomer concentration exceeds 80% by weight, it is difficult to remove the heat of polymerization and it becomes difficult to control the polymerization reaction.

  As the polymerization initiator used in Step II according to the sixth method for producing a monolith, a compound that generates radicals by heat or light irradiation is suitably used. The polymerization initiator is preferably oil-soluble. Specific examples of the polymerization initiator include 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), 2,2′-azobis (2-methylbutyro). Nitrile), 2,2′-azobis (4-methoxy-2,4-dimethylvaleronitrile), dimethyl 2,2′-azobisisobutyrate, 4,4′-azobis (4-cyanovaleric acid), 1,1 ′ -Azobis (cyclohexane-1-carbonitrile), benzoyl peroxide, lauroyl peroxide, tetramethylthiuram disulfide and the like. The amount of the polymerization initiator used varies greatly depending on the type of monomer, polymerization temperature, etc., but can be used in a range of about 0.01 to 5% with respect to the total amount of vinyl monomer and crosslinking agent.

  In step III according to the sixth method for producing a monolith, the mixture obtained in step II is left standing, and polymerization is carried out in the presence of the monolith intermediate (6) obtained in step I. This is a step of obtaining a sixth monolith having a skeleton thicker than the skeleton of (6) and having a skeleton surface layer having a porous structure.

  In the production of the sixth monolith, the internal volume of the reaction vessel is not particularly limited as long as the monolith intermediate (6) is large enough to be present in the reaction vessel, and the monolith intermediate (6) is contained in the reaction vessel. When the is placed, the gap may be formed around the monolith in plan view, or the monolith intermediate (6) may enter the reaction vessel without any gap. Of these, the monolith after polymerization does not receive any pressure from the inner wall of the vessel and enters the reaction vessel without any gap, so that the monolith is not distorted and the reaction raw materials are not wasted and efficient. Even when the internal volume of the reaction vessel is large and there are gaps around the monolith after polymerization, the vinyl monomer and the second cross-linking agent are adsorbed and distributed on the monolith intermediate, A particle aggregate structure is not generated in the gap portion.

  In step III according to the sixth method for producing a monolith, the monolith intermediate (6) is placed in a state of being impregnated with the mixture (solution) in the reaction vessel. As described above, the blending ratio of the mixture obtained in Step II and the monolith intermediate (6) is 3 to 70 times by weight, preferably 4 to 4 times by weight, relative to the monolith intermediate (6). It is preferable to blend so as to be 50 times. Thereby, it is possible to obtain a monolith having a suitable opening diameter and having a porous structure introduced into the skeleton. In the reaction vessel, the vinyl monomer and the second cross-linking agent in the mixture are adsorbed and distributed on the skeleton of the monolith intermediate (6) that is allowed to stand, and polymerization proceeds in the skeleton of the monolith intermediate. Although the details of the reason why a porous structure is formed in the process in which the polymerization proceeds are unknown, if the vinyl monomer concentration is extremely high or the amount of the crosslinking agent is extremely small, the progress of the polymerization becomes non-uniform and the crosslinked structure This is considered to be due to uneven distribution.

  In step III according to the sixth method for producing a monolith, various polymerization conditions can be selected depending on the type of monomer and the type of initiator. For example, when 2,2′-azobis (isobutyronitrile), 2,2′-azobis (2,4-dimethylvaleronitrile), benzoyl peroxide, lauroyl peroxide, or the like is used as an initiator, an inert atmosphere What is necessary is just to heat-polymerize for 1 to 48 hours at 30-100 degreeC in a lower sealed container. By the heat polymerization, the vinyl monomer adsorbed and distributed on the skeleton of the monolith intermediate (6) and the second crosslinking agent are polymerized in the skeleton to thicken the skeleton and form a porous structure in the skeleton. After the completion of the polymerization, the contents are taken out and extracted with a solvent such as methanol or acetone for the purpose of removing unreacted vinyl monomer and organic solvent to obtain a sixth monolith having a specific skeleton structure.

  The basic structure of the sixth monolith obtained in step III according to the sixth monolith manufacturing method is the structure shown in FIG.

  The sixth monolith ion exchanger is obtained by performing an IV step for introducing an ion exchange group into the sixth monolith obtained in the step III. In step IV, since the ion exchange group is introduced into the sixth monolith obtained in step III, the porous structure of the monolith ion exchanger can be strictly controlled.

  The method for introducing an ion exchange group into the sixth monolith is the same as the method for introducing an ion exchange group into the first monolith.

<Description of platinum group metal supported catalyst>
The platinum group metal-supported catalyst of the present invention is a platinum group metal-supported catalyst in which platinum group metal particles having an average particle diameter of 1 to 100 nm are supported on a monolithic organic porous body or a monolithic organic porous ion exchanger. A platinum group metal-supported catalyst, wherein the platinum group metal particles have a degree of uniformity of 10 or less, and the amount of the platinum group metal particles supported is 0.004 to 20% by weight in a dry state. is there.

  The platinum group metal supported catalyst of the present invention is a monolithic organic porous material, for example, any one of the first monolith to the sixth monolith and the first monolith ion exchanger to the sixth monolith ion exchanger. A platinum group metal-supported catalyst in which platinum group metal particles having a particle diameter of 1 to 100 nm are supported.

  The platinum group metal according to the present invention is ruthenium, rhodium, palladium, osmium, iridium, or platinum. These platinum group metals may be used alone or in combination of two or more metals, and more than one metal may be used as an alloy. Among these, platinum, palladium, and platinum / palladium alloys have high catalytic activity and are preferably used.

  The average particle diameter of the platinum group metal particles supported on the platinum group metal catalyst support of the present invention is 1 to 100 nm, preferably 1 to 50 nm, and more preferably 1 to 20 nm. If the average particle diameter is less than 1 nm, the possibility that the platinum group metal particles will be detached from the carrier increases, which is not preferable. On the other hand, if the average particle diameter exceeds 100 nm, the surface area per unit mass of the metal decreases. This is not preferable because the catalytic effect cannot be obtained efficiently. In the present invention, the average particle diameter of the platinum group metal particles is determined by image analysis of a TEM image obtained by transmission electron microscope (TEM) analysis. Specifically, first, the surface of the platinum group metal supported catalyst is subjected to TEM analysis. Next, in the obtained TEM image, one visual field in which the number of particles is 200 or more is arbitrarily selected, and the TEM image of the visual field is image-analyzed to measure the particle diameter of all particles in the visual field. When the number of platinum group metal particles carried in one field is less than 200, two or more fields of view are arbitrarily selected, and the particle size of all particles in the selected two or more fields of view is Measure. Next, the average particle diameter of the platinum group metal particles is expressed by the following formula: “average particle diameter of platinum group metal particles (nm) = total particle diameter of all measured particles (nm) / number of measured particles (pieces)” To calculate.

The uniformity number of the platinum group metal particles supported on the platinum group metal catalyst support of the present invention is 10 or less, preferably 5 or less. When the degree of uniformity of the platinum group metal particles is in the above range, the catalytic activity is increased. In the present invention, the degree of uniformity of the platinum group metal particles is determined by image analysis of a TEM image obtained by transmission electron microscope (TEM) analysis. Specifically, first, the surface of the platinum group metal supported catalyst is subjected to TEM analysis. Next, in the obtained TEM image, one visual field in which the number of particles is 200 or more is arbitrarily selected, and the TEM image of the visual field is image-analyzed to measure the particle diameter of all particles in the visual field. When the number of platinum group metal particles carried in one field is less than 200, two or more fields of view are arbitrarily selected, and the particle size of all particles in the selected two or more fields of view is Measure. Subsequently, the measured particles are arranged in order of particle size from the largest particle size to the smallest particle size, and a distribution for each 1 nm is obtained. Then, the median value of each distribution band is set as the representative particle diameter of the distribution band, and is integrated from the particles of the maximum particle diameter, and the representative particle diameter of the distribution band including particles whose number is 40% with respect to the total number of particles. (Nm) (hereinafter referred to as “40% particle diameter”) and the representative particle diameter of the distribution band including particles that are 90% of the total number of particles, with the total particle number being integrated. (Nm) (hereinafter referred to as “90% particle diameter”), and the degree of uniformity is calculated by the following formula:
Uniformity = 40% particle diameter (nm) −90% particle diameter (nm)
Calculate with

The supported amount of platinum group metal particles in the platinum group metal supported catalyst of the present invention ((platinum group metal particles / platinum group metal supported catalyst in dry state) × 100) is 0.004 to 20% by weight, preferably 0.8. 005 to 15% by weight. When the amount of platinum group metal particles supported is less than 0.004% by weight, the effect of decomposing hydrogen peroxide or the effect of removing dissolved oxygen becomes insufficient. On the other hand, when the amount of platinum group metal particles is more than 20% by weight, metal elution into water is observed, which is not preferable.
Moreover, since the platinum group metal-supported catalyst of the present invention has high hydrogen peroxide decomposition performance or dissolved oxygen removal performance, even if the water flow rate is as high as SV = 2000 to 40000 h ⁻¹ , a small amount of platinum group metal particles are supported. By amount, it exhibits excellent hydrogen peroxide decomposition effect or dissolved oxygen removal effect. When the water flow rate is SV = 2000 to 40000 h ⁻¹ , the supported amount of platinum group metal particles is preferably 0.004 to 2.0% by weight.

<Method for producing platinum group metal supported catalyst>
The method for producing a platinum group metal-supported catalyst of the present invention comprises a fluid containing platinum group metal particles having an average particle size of 1 to 100 nm and a homogeneity of 10 or less, for example, an average particle size of 1 to 100 nm and By contacting the monolithic organic porous material or the monolithic organic porous ion exchanger with a supercritical fluid containing platinum group metal particles having a homogeneity of 10 or less, the monolithic organic porous material or the monolithic organic porous material is obtained. A platinum group metal supported catalyst manufacturing method comprising a platinum group metal supported step of obtaining a platinum group metal supported catalyst by supporting the platinum group metal particles on a porous ion exchanger.

  In the platinum group metal-supporting step according to the method for producing a platinum group metal-supported catalyst of the present invention, a fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less, for example, an average particle diameter Is a monolithic organic porous body or monolithic organic porous ion exchanger to be contacted with a supercritical fluid containing platinum group metal particles having a homogeneity of 10 or less, and the skeleton of the organic porous body is A monolithic organic porous body or a monolithic organic porous ion exchanger that is formed of an organic polymer and has a large number of communication holes that serve as channels of water to be treated in the skeleton. For example, the first monolith to the first 6 monoliths and first to sixth monolith ion exchangers.

A fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less, for example, platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less. A method of bringing a monolith or a monolith ion exchanger into contact with a supercritical fluid will be described by exemplifying a case where the fluid is composed of supercritical carbon dioxide.
A supercritical fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less is an organic material, and platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less are organic. It is obtained by mixing a platinum group metal colloid solution dispersed in a solvent and supercritical carbon dioxide. By dispersing the platinum group metal particles in carbon dioxide in a supercritical state, a supercritical fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less is obtained.
(I) First, a platinum group metal particle having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less and a monolith or a monolith ion exchanger are placed in a pressure vessel, and the pressure vessel is sealed. Next, carbon dioxide is introduced into the pressure vessel until a predetermined pressure is reached, and heated to a predetermined temperature, thereby bringing the carbon dioxide in the pressure vessel into a supercritical state. Next, this supercritical state is maintained for a predetermined time.
(Ii) First, the pressure vessel is filled with a monolith or a monolith ion exchanger. In another cylindrical catalyst-filled container, platinum group metal particles having an average particle diameter of 1 to 100 nm and a uniformity degree of 10 or less are placed and sealed. Next, carbon dioxide is introduced into the pressure vessel until a predetermined pressure is reached, and heated to a predetermined temperature, thereby bringing the carbon dioxide in the pressure vessel into a supercritical state. Next, carbon dioxide is introduced into the cylindrical catalyst filling container until a predetermined pressure is reached, and the carbon dioxide in the cylindrical catalyst filling container is brought to a supercritical state by heating to a predetermined temperature. Next, while supplying the supercritical carbon dioxide containing platinum group metal particles in the cylindrical catalyst filling container from one end of the pressure vessel, the carbon dioxide is discharged from the other end of the pressure vessel, The supercritical carbon dioxide containing platinum group metal particles is allowed to pass through the pores of the monolith or monolith ion exchanger filled in.

  In the platinum group metal colloid solution in which the platinum group metal particles are dispersed in an organic solvent, the average particle diameter and the uniformity degree of the platinum group metal particles in the colloid solution are obtained by analyzing a TEM image obtained by transmission electron microscope (TEM) analysis. It is obtained by image analysis. Specifically, first, one drop of the colloidal solution is dropped onto a transmission electron microscope mesh (for example, a formal support membrane mesh manufactured by Oken Shoji) and allowed to dry naturally. Then, it observes with TEM and obtains a TEM image. The obtained TEM image is image-analyzed to determine the average particle diameter and the degree of uniformity of the platinum group metal particles in the colloidal solution. The average of the platinum group metal particles supported on the platinum group metal supported catalyst of the present invention is used. This is the same as the method for obtaining the particle diameter and the uniformity degree.

  In the platinum group metal loading process using a supercritical fluid, the pressure and temperature when the monolith or the monolith ion exchanger is brought into contact with the supercritical fluid containing the platinum group metal particles are in the range of the pressure and temperature at which the supercritical state is reached. Therefore, it is appropriately selected. For example, in the case of supercritical carbon dioxide, the temperature is selected in the range of 0 to 120 ° C., and the pressure that becomes the supercritical state at the selected temperature is selected as the pressure. For example, the conditions of 40 to 80 ° C. and 20 to 30 MPa are selected.

  The content of platinum group metal particles in a fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less is obtained by performing a platinum group metal support step. The amount of platinum group metal particles supported in the catalyst is appropriately selected so as to be 0.004 to 20% by weight, preferably 0.005 to 15% by weight.

  In the platinum group metal loading process using a supercritical fluid, the contact time when the monolith or monolith ion exchanger is brought into contact with the supercritical fluid containing platinum group metal particles is the pores in the monolith or monolith ion exchanger. It is sufficient that the time is sufficient for the supercritical fluid to permeate, and is appropriately selected. Usually, it is 0.2 to 48 hours.

  In the platinum group metal supporting step using the supercritical fluid, after bringing the monolith or the monolith ion exchanger into contact with the supercritical fluid containing the platinum group metal particles, the pressure in the system is reduced to normal pressure, A platinum group metal-supported catalyst in which platinum group metal particles having a predetermined particle property are supported on a monolith or a monolith ion exchanger is obtained. Moreover, after performing a platinum group metal carrying | support process, the obtained platinum group metal carrying | support catalyst can be washed with water, dried, etc. as needed.

<Method for Producing Hydrogen Peroxide Decomposition Treatment Water>
In the method for producing hydrogen peroxide decomposition treated water of the present invention, the platinum group metal-supported catalyst of the present invention is brought into contact with water to be treated containing hydrogen peroxide, so that the water in the water to be treated containing hydrogen peroxide is treated. This is a method for producing hydrogen peroxide decomposition treated water that decomposes and removes hydrogen oxide.

  The water to be treated containing hydrogen peroxide is not particularly limited as long as it contains hydrogen peroxide. For example, ultrapure water used for manufacturing electronic components such as semiconductor manufacturing and for cleaning electronic device manufacturing equipment. In the production of water, water generated by various processes therein can be mentioned, and specifically, water after performing an ultraviolet oxidation process for decomposing organic substances in the water. In addition, as the water to be treated containing hydrogen peroxide, in addition to the treatment liquid or treatment water obtained by adding hydrogen peroxide to the waste water system, and performing oxidation, reduction, sterilization and washing, these treatment liquids or The waste liquid or waste water after processing using treated water is mentioned. For example, in order to collect and reuse cleaning wastewater containing hydrogen peroxide discharged from the semiconductor manufacturing process and cleaning wastewater containing organic matter discharged from the semiconductor manufacturing process as ultrapure water, ultraviolet rays are used in the presence of hydrogen peroxide. Treated water obtained by oxidative decomposition of organic matter by irradiation, treated water obtained by decomposing organic matter using Fenton reagent, reverse osmosis membrane, waste water after sterilizing or washing ultrafiltration membrane with hydrogen peroxide, Examples thereof include treated water obtained by reducing wastewater containing hexavalent chromium with hydrogen peroxide.

  The concentration of hydrogen peroxide in the water to be treated containing hydrogen peroxide is not particularly limited, but is usually 0.01 to 100 mg / L. In the ultrapure water production subsystem, the hydrogen peroxide concentration is typically 10-50 μg / L. When the hydrogen peroxide concentration exceeds 100 mg / L, the base monolith and the monolith ion exchanger are likely to deteriorate.

  The method for bringing the water to be treated containing hydrogen peroxide into contact with the platinum group metal supported catalyst of the present invention is not particularly limited. For example, the catalyst packed tower is packed with the platinum group metal supported catalyst of the present invention, Examples include a method of supplying water to be treated containing hydrogen peroxide to the platinum group metal-supported catalyst of the present invention by supplying the liquid to be treated containing hydrogen peroxide to the catalyst packed tower.

For the method, the platinum group metal supported catalyst of the present invention, the treatment water containing hydrogen peroxide, SV = 2000~40000h ^-1, preferably be passing water SV = 5000~20000h ^-1 . When the platinum group metal-supported catalyst of the present invention is used, hydrogen peroxide can be decomposed and removed even when the water to be treated is passed with a large SV such that the SV exceeds 2000 h- ¹ . Furthermore, even if SV is 10000h- ¹ , if the platinum group metal-supported catalyst of the present invention is used, hydrogen peroxide can be decomposed, and the platinum group metal-supported catalyst of the present invention can be used as a particulate anion exchange resin. It shows outstanding performance that far exceeds the processing limit of conventional supported catalysts supporting platinum group metal nanoparticles. Water flow rate of the for-treatment water containing hydrogen peroxide to the platinum group metal supported catalyst of the present invention is not particularly limited, preferably SV = 2000~40000h ^-1, particularly preferably SV = 5000~20000h ^-1 It is. In addition, since the platinum group metal supported catalyst of the present invention has a remarkably high hydrogen peroxide decomposition ability, it is not necessary to dare to set the water flow rate to an area of less than SV = 2000 h ^−1, but the water flow rate is set to SV = 2000 h ^−. It may be less than ^one region, even if the water flow rate was region below SV = 2000h ^-1, platinum group metal supported catalyst of the present invention exhibits excellent hydrogen peroxide decomposition ability. On the other hand, when SV exceeds 40000h- ¹ , the water flow differential pressure tends to be too large.

  Furthermore, since the platinum group metal-supported catalyst of the present invention has a remarkably high hydrogen peroxide decomposition ability, hydrogen peroxide can be decomposed and removed even if the packed bed height of the catalyst is reduced. The packed bed height of the platinum group metal supported catalyst of the present invention is preferably 5 to 1000 mm, particularly preferably 10 to 500 mm, and more preferably 10 to 100 mm. When the packed bed height of the platinum group metal supported catalyst is less than 5 mm, the mechanical strength of the catalyst layer is likely to be insufficient, and hydrogen peroxide is liable to leak. On the other hand, when the catalyst layer height of the platinum group metal catalyst exceeds 1000 mm, the water flow differential pressure increases.

  The hydrogen peroxide concentration in the treated water obtained by performing the method for producing hydrogen peroxide-decomposed treated water of the present invention is not particularly limited, but is usually 10 μg / L to 100 mg / L (10 ppb to 100 ppm). When the hydrogen peroxide concentration exceeds 100 mg / L, the carrier monolith and the monolith ion exchanger are likely to deteriorate. In addition, the density | concentration of the hydrogen peroxide contained in the to-be-processed water of the subsystem which comprises the manufacturing apparatus of ultrapure water which is a kind of to-be-processed water containing hydrogen peroxide is 10-50 microgram / L (10 ˜50 ppb).

<Method for Producing Dissolved Oxygen Removal Water of the Present Invention>
The method for producing treated water for removing dissolved oxygen according to the present invention comprises reacting dissolved oxygen and hydrogen in water to be treated containing oxygen in the presence of the platinum group metal-supported catalyst of the present invention to produce water. A method for producing water for removing dissolved oxygen, which removes dissolved oxygen from water to be treated containing oxygen.

  The water to be treated containing oxygen is not particularly limited as long as it contains oxygen. For example, the manufacture of electronic parts such as semiconductor manufacturing and the manufacture of ultrapure water for cleaning electronic parts manufacturing equipment, etc. The raw water used in the production process or various kinds of water in the production process thereof, specifically, circulating water of the ultrapure water production subsystem, for example, the outlet water of the ultraviolet oxidizer. Other examples of water to be treated containing dissolved oxygen include water used at power plants, boiler water and cooling water used at various factories.

  Although the dissolved oxygen concentration in the to-be-treated water containing oxygen is not particularly limited, it is usually 0.01 to 10 mg / L.

  The amount of hydrogen reacted with dissolved oxygen is not particularly limited, but is 1 to 10 equivalents, preferably 1.1 to 5 equivalents of the oxygen concentration.

  The method for reacting dissolved oxygen and hydrogen in the water to be treated containing oxygen in the presence of the platinum group metal supported catalyst of the present invention is not particularly limited. For example, the platinum group metal of the present invention is added to a catalyst packed tower. The supported catalyst is packed, and the treatment liquid containing oxygen is supplied to the catalyst packed tower, and hydrogen gas is injected into the supply pipe of the treatment liquid to dissolve in the platinum group metal supported catalyst of the present invention. Examples include a method of passing hydrogen and water to be treated containing dissolved oxygen.

For the above method, the platinum group metal supported catalyst of the present invention, the treatment water containing oxygen, SV = 2000~40000h ^-1, preferably be passing water SV = 5000~20000h ^-1. When the platinum group metal-supported catalyst of the present invention is used, dissolved oxygen can be removed even when the water to be treated is passed through with a large SV such that SV exceeds 2000 h- ¹ . Furthermore, even if SV is 10000h- ¹ , if the platinum group metal-supported catalyst of the present invention is used, dissolved oxygen can be removed. The platinum group metal-supported catalyst of the present invention can be used as a particulate anion exchange resin. Excellent performance, far exceeding the processing limit of conventional supported catalysts supporting group metal nanoparticles. Water flow rate of the for-treatment water containing oxygen to platinum group metal supported catalyst of the present invention is not particularly limited, is preferably SV = 2000~40000h ^-1, particularly preferably SV = 5000~20000h ^-1 . In addition, since the platinum group metal supported catalyst of the present invention has a remarkably high dissolved oxygen removal capability, the water flow rate greatly exceeds the processing limit of the conventional supported catalyst in which platinum group metal nanoparticles are supported on the particulate anion exchange resin. Even if the water to be treated is passed, dissolved oxygen in the water to be treated can be decomposed.

  Furthermore, since the platinum group metal supported catalyst of the present invention has a remarkably high dissolved oxygen removing ability, it is possible to remove dissolved oxygen even if the packed bed height of the catalyst is made thin.

  It is preferable that the dissolved oxygen concentration in the treated water obtained by performing the method for producing treated water for removing dissolved oxygen of the present invention is 10 μg / L or less.

  The platinum group metal-supported catalyst of the present invention has platinum group metal particles supported on a monolith or monolith ion exchanger, and the average particle diameter of the supported platinum group metal particles is as small as 1 to 100 nm, and the degree of uniformity. Since the particle diameter is uniform at 10 or less, the contact efficiency between the water to be treated containing hydrogen peroxide, dissolved oxygen and the like and the platinum group metal catalyst is significantly higher than that of the conventional granular platinum group metal supported catalyst. Therefore, the platinum group metal-supported catalyst of the present invention has a remarkably high ability to decompose hydrogen peroxide and dissolved oxygen. Therefore, even if the packed bed height of the catalyst is reduced, hydrogen peroxide and dissolved oxygen in the water to be treated are decomposed and removed. can do.

In particular, the platinum group metal-supported catalyst of the present invention has a uniformity number of 10 or less even when the amount of platinum group metal particles supported is as small as 0.004 to 2.0% by weight. Since contact efficiency with a metal catalyst becomes high, a water flow rate can be made high with 2000-40000h- ¹ .

Further, since the platinum group metal-supported catalyst of the present invention is a monolith or a monolith ion exchanger, the monolith or monolith ion is supported in the step of supporting platinum group metal particles as compared with a catalyst in which the support is an inorganic porous body. The platinum group metal particles can be supported in a swollen state of the exchanger, and the platinum group metal particles can be held in the support by returning to the original state after the support. Therefore, the inorganic porous material is used as the support. It is possible to provide a catalyst in which the outflow and desorption of platinum group metal particles from the carrier, which is a problem with the catalyst, do not become a problem.
In addition, since the carrier is a monolith or a monolith ion exchanger, the method for producing a platinum group metal-supported catalyst of the present invention has a monolith in a step of supporting platinum group metal particles compared to a catalyst in which the carrier is an inorganic porous body. Alternatively, the platinum group metal particles can be supported in a swollen state of the monolith ion exchanger, and the platinum group metal particles can be held in the support by returning to the original state after the support. This is a production method capable of providing a catalyst in which the outflow or desorption of platinum group metal particles from the carrier, which is a problem with the catalyst used as the carrier, does not matter.

  Further, in the method for producing a platinum group metal-supported catalyst of the present invention, a platinum group metal particle, such as platinum, used when preparing a fluid containing platinum group metal particles, for example, a supercritical fluid containing platinum group metal particles, is used. The particle properties of the platinum group metal particles supported on the platinum group metal supported catalyst can be controlled by the particle properties of the platinum group metal particles in the group III metal colloid liquid. Therefore, according to the method for producing a platinum group metal-supported catalyst of the present invention, it is easy to control the particle properties of the platinum group metal particles supported on the monolith or the monolith ion exchanger, the average particle diameter is 1 to 100 nm, and The uniformity number can be 10 or less.

  On the other hand, in a production method in which a platinum group metal ion is bound to a carrier having an ion exchange group by ion exchange and the ions are reduced to obtain a platinum group metal supported catalyst, all of the platinum group metal ions are completely reduced. It is unclear whether it is present or may remain as an ion. In addition, platinum group metal particles generated by reduction are unstable and may cause secondary aggregation. When secondary agglomeration occurs, the particle surface area decreases and the catalytic activity decreases. Therefore, in order to obtain high catalytic activity, it is necessary to support the platinum group metal by a method that does not cause secondary aggregation. In addition, in the catalyst in which secondary aggregation exists, small particles that are not aggregated and large particles that are aggregated are mixed. Therefore, the uniformity number of the supported platinum group metal particles is not 10 or less.

(Example)
Next, the present invention will be specifically described by way of examples, but this is merely an example and does not limit the present invention.

Example 1
<Production of platinum group supported catalyst 1>
(Step I; production of monolith intermediate (4) A)
5.29 g of styrene, 0.28 g of divinylbenzene, 1.39 g of sorbitan monooleate (hereinafter abbreviated as SMO) and 0.26 g of 2,2′-azobis (isobutyronitrile) were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / SMO / 2,2′-azobis (isobutyronitrile) mixture was added to 180 g of pure water, and a vacuum stirring defoaming mixer (manufactured by EM Co.) as a planetary stirring device. Was used under reduced pressure in a temperature range of 5 to 20 ° C. to obtain a water-in-oil emulsion. This emulsion was quickly transferred to a reaction vessel and allowed to polymerize at 60 ° C. for 24 hours in a static state after sealing. After completion of the polymerization, the content was taken out, extracted with methanol, and then dried under reduced pressure to produce Monolith Intermediate (4) A having a continuous macropore structure.
When the internal structure of the monolith intermediate (dry body) obtained in this way was observed with an SEM image (FIG. 7), the wall portion separating two adjacent macropores was very thin and rod-shaped, but the open cell structure The average diameter of the openings (mesopores) where the macropores overlap with each other as measured by the mercury intrusion method was 70 μm in the dry state, and the total pore volume in the dry state was 17.8 ml / g.

(Production of fourth monolith A)
Next, 39.2 g of styrene, 0.8 g of divinylbenzene, 60 g of 1-decanol, and 0.8 g of 2,2′-azobis (2,4-dimethylvaleronitrile) were mixed and dissolved uniformly (step II). Next, the monolith intermediate (4) A was cut into a disk shape having a diameter of 70 mm and a thickness of about 30 mm to obtain 2.4 g. The separated monolith intermediate is placed in a reaction vessel having an inner diameter of 75 mm, immersed in the styrene / divinylbenzene / 1-decanol / 2,2′-azobis (2,4-dimethylvaleronitrile) mixture, and removed in a vacuum chamber. After bubbling, the reaction vessel was sealed and allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the monolith-like contents having a thickness of about 60 mm were taken out, soxhlet extracted with acetone, and then dried under reduced pressure at 85 ° C. overnight to obtain a fourth monolith A (step III).

FIG. 5 shows the result of observing the internal structure of the fourth monolith A (dried body) thus obtained by SEM. As is apparent from FIG. 5, the fourth monolith A had a co-continuous structure in which the skeleton and the vacancies were each three-dimensionally continuous and the two phases were intertwined. Moreover, the average thickness of the skeleton measured from the SEM image was 8 μm. Moreover, the average diameter in the dry state of the three-dimensionally continuous pores of the monolith measured by the mercury intrusion method was 18 μm, and the total pore volume in the dry state was 2.0 ml / g.
In addition, the change (expansion rate) when the fourth monolith A in the dry state is wetted with water is 1.3 times, and the fourth monolith A in the water wet state estimated from this expansion rate is obtained. The average thickness of the skeleton was 10 μm, and the average diameter of the pores was 23 μm.

(Production of fourth monolith anion exchanger A)
The fourth monolith A produced by the above method was cut into a disk shape having a diameter of 70 mm and a thickness of about 15 mm. To this, 1400 ml of dimethoxymethane and 20 ml of tin tetrachloride were added, and 560 ml of chlorosulfuric acid was added dropwise under ice cooling. After completion of the dropping, the temperature was raised and the reaction was carried out at 35 ° C. for 5 hours to introduce a chloromethyl group. After completion of the reaction, the mother liquor was extracted with a siphon, washed with a mixed solvent of THF / water = 2/1, and further washed with THF. To this chloromethylated monolithic organic porous material, 1000 ml of THF and 600 ml of a 30% trimethylamine aqueous solution were added and reacted at 60 ° C. for 6 hours. After completion of the reaction, the product was washed with a methanol / water mixed solvent and then washed with pure water to obtain a fourth monolith anion exchanger A.

  The swelling ratio before and after the reaction of the obtained fourth monolith anion exchanger A was 1.6 times, and the anion exchange capacity per volume was 0.44 mg equivalent / ml in a water-wet state. The average diameter of the continuous pores of the monolith ion exchanger in the water-wet state was estimated to be 29 μm from the value of the monolith in the dry state and the rate of change before and after the introduction of anion exchange groups (swelling rate: 1.6 times). The average thickness of the skeleton was 13 μm. The total pore volume in the dry state was 2.5 ml / g.

  Next, in order to confirm the distribution state of the quaternary ammonium groups in the fourth monolith anion exchanger A, the fourth monolith anion exchanger A is treated with an aqueous hydrochloric acid solution to form a chloride form, and then the skeleton is formed by EPMA When the distribution state of chloride ions on the surface and inside the skeleton was observed, the chloride ions were uniformly distributed not only on the skeleton surface of the fourth monolith anion exchanger A but also inside the skeleton. It was confirmed that was uniformly introduced into the monolith anion exchanger.

(Adjustment of platinum group metal supported catalyst 1)
The fourth monolith anion exchanger A was ion-exchanged into a Cl form, cut into a cylindrical shape having a diameter of 30 mm and a thickness of 15 mm in a water-swelled state, and dried under reduced pressure. The weight of the monolith anion exchanger after drying was 1.6 g. This dried monolith anion exchanger was immersed in water and again brought into a water swollen state.
Next, the water-swollen monolith anion exchanger and 5 ml of palladium nanocolloid liquid (4% by weight of palladium) were placed in a pressure vessel and sealed. The sealed pressure vessel was placed in a constant temperature bath at 40 ° C. Carbon dioxide was introduced into the pressure vessel until it reached 25 MPa. The introduction was stopped when the pressure reached 25 MPa, and the state was maintained for 1 hour. After 1 hour, the pressure vessel was opened to release carbon dioxide. The monolith anion exchanger carrying palladium was taken out from the pressure vessel. The taken-out palladium-supported monolith anion exchanger was regenerated with 1.0N sodium hydroxide to form OH to obtain a platinum group metal-supported catalyst 1.
One drop of the palladium nanocolloid solution used above was dropped on a transmission electron microscope mesh (manufactured by Oken Shoji Co., Ltd., a formal support membrane mesh) and allowed to dry naturally. Next, observation with a transmission electron microscope (TEM) to obtain a TEM image, image analysis of the obtained TEM image, measurement of the particle diameter of the palladium particles in the observed visual field, in the palladium nanocolloid solution The particle size distribution of palladium particles was obtained. Table 1 shows the particle size distribution of the palladium particles in the obtained palladium nanocolloid solution. The number of uniformity obtained from Table 1 is 2. Moreover, the average particle diameter of the palladium particle | grains in the palladium nanocolloid solution calculated | required from the image analysis of the obtained TEM image was 4.0 nm.
The amount of palladium supported on the platinum group metal supported catalyst 1 in the dry state was 2.0% by weight. The particle diameter of the palladium particles supported on the platinum group metal-supported catalyst 1 is observed with a transmission electron microscope, a TEM image is obtained, the obtained TEM image is image-analyzed, and the particles of palladium particles in the observed visual field The particle size distribution of palladium particles supported on the platinum group metal supported catalyst 1 was obtained by measuring the diameter. Table 2 shows the particle size distribution of the palladium particles supported on the obtained platinum group metal supported catalyst 1. The uniformity number obtained from Table 2 is 2. Moreover, the average particle diameter of the palladium particle | grains carry | supported by the platinum group metal carrying | support catalyst 1 calculated | required from the image analysis of the obtained TEM image was 5.2 nm.

<Manufacture of hydrogen peroxide decomposition treated water>
The platinum group metal supported catalyst 1 was cut out and packed in a column with an inner diameter of 10 mm, and used for evaluation of hydrogen peroxide decomposition characteristics. At this time, the packed bed height of the platinum group metal supported catalyst 1 was 13 mm.
Ultrapure water containing 15 to 30 μg / L (15 to 30 ppb) of hydrogen peroxide was passed through the filler of the platinum group metal supported catalyst 1 at SV = 20000 h ⁻¹ . After passing water for 24 hours, the solution at the outlet of the column was collected and the hydrogen peroxide concentration was measured. As a result, the hydrogen peroxide concentration is less than 1 μg / L, it is very fast, SV = 20000h ^−1, and the hydrogen peroxide is decomposed and removed even though the packed bed height of the platinum group metal supported catalyst 1 is as low as 13 mm. It had been. Next, the same processing was performed with SV = 40000 h ⁻¹ . The solution at the outlet of the column was collected and the hydrogen peroxide concentration was measured. As a result, the hydrogen peroxide concentration was 2.0 g / L, and the hydrogen peroxide was decomposed and removed.

(Example 2)
<Production of platinum group metal supported catalyst 2>
(Step I; production of monolith intermediate (4) A)
In the same manner as in Example 1, monolith intermediate (4) A was produced.
(Production of 4th monolith A)
A fourth monolith A was produced in the same manner as in Example 1.
(Production of fourth monolith anion exchanger A)
In the same manner as in Example 1, a fourth monolith anion exchanger A was produced.
(Adjustment of platinum group metal supported catalyst 2)
The fourth monolith anion exchanger A was ion-exchanged into a Cl form, cut into a cylindrical shape having a diameter of 30 mm and a thickness of 15 mm in a water-swelled state, and dried under reduced pressure. The weight of the monolith anion exchanger after drying was 1.6 g. This dried monolith anion exchanger was immersed in water and again brought into a water swollen state. Next, the water-swelled monolith anion exchanger and 5 mL of palladium nanocolloid solution (palladium 0.1 wt%) were placed in a pressure vessel and sealed. The sealed pressure vessel was placed in a constant temperature bath at 40 ° C. Carbon dioxide was introduced into the pressure vessel until it reached 25 MPa. When the pressure reached 25 MPa, the introduction was stopped and the state was maintained for 6 hours. After 6 hours, the pressure vessel was opened to release carbon dioxide. The monolith anion exchanger carrying palladium was taken out from the pressure vessel. The taken-out palladium-supported monolith anion exchanger was regenerated with 1.0N sodium hydroxide to form OH to obtain a platinum group metal-supported catalyst 2.
One drop of the palladium nanocolloid solution used above was dropped on a transmission electron microscope mesh (manufactured by Oken Shoji Co., Ltd., a formal support membrane mesh) and allowed to dry naturally. Next, observation with a transmission electron microscope (TEM) to obtain a TEM image, image analysis of the obtained TEM image, measurement of the particle diameter of the palladium particles in the observed visual field, in the palladium nanocolloid solution The particle size distribution of palladium particles was obtained. Table 3 shows the particle size distribution of the palladium particles in the obtained palladium nanocolloid solution. The uniformity number obtained from Table 3 is 2. Moreover, the average particle diameter of the palladium particle | grains in the palladium nanocolloid solution calculated | required from the image analysis of the obtained TEM image was 4.0 nm.
The amount of palladium supported on the platinum group metal supported catalyst 2 in a dry state was 0.05% by weight. The particle diameter of the palladium particles supported on the platinum group metal-supported catalyst 2 is observed with a transmission electron microscope to obtain a TEM image. The obtained TEM image is subjected to image analysis, and the particles of palladium particles in the observed visual field. The particle size distribution of palladium particles supported on the platinum group metal supported catalyst 2 was obtained by measuring the diameter. Table 4 shows the particle size distribution of the palladium particles supported on the obtained platinum group metal supported catalyst 2. The uniformity number obtained from Table 4 is 1. Moreover, the average particle diameter of the palladium particle | grains carry | supported by the platinum group metal carrying | support catalyst 2 calculated | required from the image analysis of the obtained TEM image was 4.5 nm.

<Manufacture of hydrogen peroxide decomposition treated water>
The platinum group metal supported catalyst 2 was cut out and packed in a column having an inner diameter of 10 mm, and used for evaluation of hydrogen peroxide decomposition characteristics. At this time, the packed bed height of the platinum group metal supported catalyst 2 was 14 mm.
Ultra pure water containing 15 to 30 μg / L (15 to 30 ppb) of hydrogen peroxide was passed through the packing of the platinum group metal supported catalyst 2 at SV = 10000 h ⁻¹ . After passing water for 24 hours, the solution at the outlet of the column was collected and the hydrogen peroxide concentration was measured. As a result, the hydrogen peroxide concentration is less than 1 μg / L, it is very fast as SV = 10000 h ^−1, and the hydrogen peroxide is decomposed and removed even though the packed bed height of the platinum group metal supported catalyst 2 is as low as 14 mm. It had been. Next, SV = 20000h ^{−1 was set} and the same processing was performed. The solution at the outlet of the column was collected and the hydrogen peroxide concentration was measured. As a result, the hydrogen peroxide concentration was 1.5 g / L, and hydrogen peroxide was decomposed and removed.

In Table 1, since it is a distribution band of 4 or more and less than 5 (nm) that the number with respect to the number of all particles exceeds 40% when integrated from the particles with the maximum particle size, the number with respect to the number of all particles is 40. The distribution band including particles that are% is a distribution band of 4 or more and less than 5 (nm). Since the representative particle diameter of 4 or more and less than 5 (nm) is 4.5 nm, the 40% particle diameter is 4.5 nm. In addition, since the number of particles with the maximum particle diameter exceeds 90% with respect to the number of all particles is a distribution band of 2 or more and less than 3 (nm), the number with respect to the number of all particles is 90%. The distribution band including the particles is a distribution band of 2 or more and less than 3 (nm). Since the representative particle size of 2 or more and less than 3 (nm) is 2.5 nm, the 90% particle size is 2.5 nm. From these, when calculating the uniformity degree, the following formula:
Uniformity = 40% particle size−90% particle size = 4.5−2.5 = 2
Accordingly, the uniformity degree is 2.
Similarly, when the degree of uniformity was determined from Table 2, the following formula:
Uniformity = 40% particle size−90% particle size = 5.5−3.5 = 2
Accordingly, the uniformity degree is 2.
Moreover, when the uniformity number was calculated | required from Table 3, following formula:
Uniformity = 40% particle size−90% particle size = 4.5−2.5 = 2
Accordingly, the uniformity degree is 2.
Moreover, when the degree of uniformity was determined from Table 4, the following formula:
Uniformity = 40% particle size−90% particle size = 4.5−3.5 = 1
Accordingly, the uniformity degree is 1.

Example 3
<Production of platinum group metal supported catalyst 3>
(Production of first monolith B)
19.2 g of styrene, 1.0 g of divinylbenzene, 1.0 g of sorbitan monooleate (hereinafter abbreviated as SMO) and 0.26 g of 2,2′-azobis (isobutyronitrile) were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / SMO / 2,2′-azobis (isobutyronitrile) mixture is added to 180 g of pure water, and a vacuum stirring defoaming mixer (manufactured by EM Corp.) which is a planetary stirring device. Was used under reduced pressure in a temperature range of 5 to 20 ° C. to obtain a water-in-oil emulsion. The emulsion was immediately transferred to a reaction vessel, and after sealing, it was allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the content was taken out, extracted with isopropanol, and then dried under reduced pressure to obtain a first monolith B. The monolith was a styrene / divinylbenzene copolymer containing 3.3 mol% of a crosslinking component, and was confirmed to have a continuous macropore structure by SEM observation. The SEM image is shown in FIG. The average diameter in the dry state of the opening (mesopore) where the macropores of the monolith overlapped with the macropores determined by the mercury intrusion method was 29 μm, and the total pore volume in the dry state was 8.6 ml / g.

(Production of first monolith anion exchanger B)
The first monolith B manufactured by the above method was cut into a disk shape having an outer diameter of 70 mm and a thickness of about 15 mm. To this, 1400 ml of dimethoxymethane and 20 ml of tin tetrachloride were added, and 560 ml of chlorosulfuric acid was added dropwise under ice cooling. After completion of the dropwise addition, the temperature was raised and reacted at 35 ° C. for 5 hours to introduce a chloromethyl group. After completion of the reaction, the mother liquor was extracted with a siphon, washed with a mixed solvent of THF / water = 2/1, and further washed with THF. To this chloromethylated monolith, 1000 ml of THF and 600 ml of a 30% trimethylamine aqueous solution were added and reacted at 60 ° C. for 6 hours. After completion of the reaction, the product was washed with a methanol / water mixed solvent and then washed with pure water to obtain a first monolith anion exchanger B.

  The swelling ratio before and after the reaction of the obtained first monolith anion exchanger B was 1.5 times, the anion exchange capacity per weight in the dry state was 4.3 mg equivalent / g, and the opening (mesopore) The average diameter in the dry state was 43 μm, and the total pore volume in the dry state was 13 ml / g. The average diameter of the opening of the monolith anion exchanger in the water wet state was estimated from the value of the monolith and the swelling ratio of the monolith anion exchanger in the water wet state to be 44 μm, and the total pore volume was 8.6 ml / g. Met. The differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.014 MPa / m · LV, which is a lower pressure loss than that required for practical use. It was.

  Next, in order to confirm the distribution state of the quaternary ammonium group in the first monolith anion exchanger B, the monolith anion exchanger is treated with a hydrochloric acid aqueous solution to form a chloride form, and then the distribution of chloride ions by EPMA is performed. The condition was observed. As a result, chloride ions are uniformly distributed not only on the skeleton surface of the first monolith anion exchanger B but also inside the skeleton, and quaternary ammonium groups are uniformly introduced into the monolith anion exchanger. I was able to confirm.

(Preparation of platinum group metal supported catalyst 3)
A platinum group metal supported catalyst 3 was obtained in the same manner as in Example 1 except that the first monolith anion exchanger B was used instead of the fourth monolith anion exchanger A. The average particle diameter of the palladium particles supported on the platinum group metal supported catalyst 3 was 4.5 nm, and the degree of uniformity was 2. The supported amount of palladium particles of the platinum group metal supported catalyst 3 was 2.1% by weight in a dry state.

Example 4
<Production of platinum group metal supported catalyst 4>
(Production of second monolith C)
38.8 g of vinylbenzyl chloride, 1.2 g of divinylbenzene, 60 g of 1-butanol and 0.4 g of 2,2′-azobis (2,4-dimethylvaleronitrile) were mixed and dissolved uniformly. Divinylbenzene was 2.8 mol% with respect to the total amount of vinylbenzyl chloride and divinylbenzene. Next, the vinylbenzyl chloride / divinylbenzene / 1-butanol / 2,2′-azobis (2,4-dimethylvaleronitrile) mixture was put into a polyethylene cylindrical container, purged with nitrogen three times, sealed, and allowed to stand. The polymerization was carried out at 60 ° C. for 24 hours. After completion of the polymerization, the monolith-like contents having a thickness of about 30 mm were taken out, subjected to Soxhlet extraction with acetone for 10 hours to remove unreacted monomers and 1-butanol, and then dried under reduced pressure at 85 ° C. overnight to obtain the second monolith C. Got. The diameter of the obtained cylindrical second monolith C was 76 mm.

FIG. 2 shows the result of observation by SEM of the internal structure of the second monolith C containing 2.8 mol% of the cross-linking component made of the vinylbenzyl chloride / divinylbenzene copolymer thus obtained. As is apparent from FIG. 2, it can be seen that in the second monolith C, crosslinked polyvinylbenzyl chloride particles having an average diameter of about 15 μm aggregate in a dry state to form a three-dimensional continuous skeleton portion. The maximum value (average diameter of pores) in the dry state of the pore distribution curve of the second monolith C measured by the mercury intrusion method was 60 μm. Further, the total pore volume in the dry state of the second monolith C was 1.4 ml / g.
Moreover, the change (expansion rate) when the second monolith C in the dry state is wetted with water is 1.2 times, and the second monolith C in the water wet state estimated from this expansion rate is obtained. The average diameter of the organic polymer particles was 18 μm, and the average diameter of the pores in a water-wet state was 72 μm.

(Production of second monolith anion exchanger C)
The second monolith C produced by the above method was cut into a disk shape having a thickness of about 15 mm. To this was added 1500 ml of tetrahydrofuran, heated at 40 ° C. for 1 hour, then cooled to 10 ° C. or less, 140 g of a 30% trimethylamine aqueous solution was gradually added, and the temperature was raised and reacted at 40 ° C. for 24 hours. After completion of the reaction, the product was taken out and washed with methanol and pure water in this order to obtain a second monolith anion exchanger C. The obtained second monolith anion exchanger C had a diameter of 111 mm and an anion exchange capacity per volume of 0.65 mg equivalent / ml in a water-wet state. The average diameter of the pores of the monolith anion exchanger in the water wet state was estimated from the average diameter of the pores of the monolith in the dry state and the change before and after the introduction of the anion exchange group (swelling ratio: 1.5 times). Yes, the average diameter of the organic polymer particles of the monolith anion exchanger in the water wet state was estimated from the average diameter of the organic polymer particles of the monolith in the dry state and the change (swelling ratio) before and after the introduction of the anion exchange group, and was 23 μm. It was. Further, the total pore volume in the dry state was 1.4 ml / g. In addition, the differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.010 MPa / m · LV, which is a low pressure loss lower than that required for practical use. It was.

  Next, in order to confirm the distribution state of the quaternary ammonium groups in the second monolith anion exchanger C, the distribution state of chloride ions was observed by EPMA. As a result, the quaternary ammonium groups were uniformly distributed on the surface of the monolith anion exchanger. It was found that it was introduced. Moreover, when the distribution state in the cross-section (thickness) direction of the monolith anion exchanger of chloride ions was observed by EPMA, it was found that quaternary ammonium groups were uniformly introduced also in the cross-sectional direction. From this, it was found that in the obtained second monolith anion exchanger C, quaternary ammonium groups were uniformly introduced into the surface of the porous body and inside the skeleton.

(Preparation of platinum group metal supported catalyst 4)
A platinum group metal supported catalyst 4 was obtained in the same manner as in Example 1 except that the second monolith anion exchanger C was used instead of the fourth monolith anion exchanger A. The average particle diameter of the palladium particles supported on the platinum group metal supported catalyst 4 was 4.2 nm, and the degree of uniformity was 2. The supported amount of palladium particles of the platinum group metal supported catalyst 4 was 1.8% by weight in a dry state.

(Example 5)
<Production of platinum group metal supported catalyst 5>
(Step I; production of monolith intermediate (3))
19.9 g of styrene, 0.4 g of divinylbenzene, 1.0 g of sorbitan monooleate (hereinafter abbreviated as SMO) and 0.26 g of 2,2′-azobis (isobutyronitrile) were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / SMO / 2,2′-azobis (isobutyronitrile) mixture is added to 180 g of pure water containing 1.8 ml of THF, and a vacuum stirring defoaming mixer which is a planetary stirring device. (EM Co., Ltd.) was used and stirred under reduced pressure in a temperature range of 5 to 20 ° C. to obtain a water-in-oil emulsion. The emulsion was immediately transferred to a reaction vessel, and after sealing, it was allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the content was taken out, extracted with isopropanol, and then dried under reduced pressure to produce monolith intermediate (3) D having a continuous macropore structure. The average diameter in the dry state of the opening (mesopore) where the macropores and macropores of the monolith intermediate (3) D measured by the mercury intrusion method are 56 μm, and the total pore volume in the dry state is 7.5 ml / g. Met.

(Production of third monolith D)
Next, 49.0 g of styrene, 1.0 g of divinylbenzene, 50 g of 1-decanol, and 0.5 g of 2,2′-azobis (2,4-dimethylvaleronitrile) were mixed and dissolved uniformly (step II). Next, the monolith intermediate (3) D was cut into a disk shape having an outer diameter of 70 mm and a thickness of about 20 mm, and 7.6 g was collected. The separated monolith intermediate is put in a reaction vessel having an inner diameter of 90 mm, immersed in the styrene / divinylbenzene / 1-decanol / 2,2′-azobis (2,4-dimethylvaleronitrile) mixture, and removed in a vacuum chamber. After bubbling, the reaction vessel was sealed and allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the monolith-like contents having a thickness of about 30 mm were taken out, subjected to Soxhlet extraction with acetone, and then dried under reduced pressure at 85 ° C. overnight to obtain a third monolith D (step III).

  FIG. 3 shows the result of observing the internal structure of the third monolith D (dry body) containing 1.3 mol% of the cross-linking component made of the styrene / divinylbenzene copolymer by SEM. . The SEM image in FIG. 3 is an image at an arbitrary position on the cut surface obtained by cutting the monolith at an arbitrary position. As is clear from FIG. 3, the monolith has a continuous macropore structure, the skeleton constituting the continuous macropore structure is thick, and the wall portions constituting the skeleton are thick.

Next, the SEM image obtained by cutting the obtained third monolith D at a position different from the above position excluding subjectivity, the thickness of the wall part and the skeleton part area appearing in the cross section from a total of three points. It was measured. The wall thickness was an average of 8 points obtained from one SEM photograph, and the skeleton area was determined by image analysis. The wall portion has the above definition. Moreover, the skeleton part area was shown by the average of three SEM images. As a result, the average thickness of the wall portion in the dry state was 30 μm, and the skeleton area represented by the cross section was 28% in the SEM image. Moreover, the average diameter in the dry state of the opening of the third monolith D measured by the mercury intrusion method was 31 μm, and the total pore volume in the dry state was 2.2 ml / g.
In addition, the change (expansion rate) when the third monolith D in the dry state is wetted with water is 1.3 times, and the third monolith C in the water wet state estimated from this expansion rate is obtained. The average diameter of the openings was 40 μm.

(Production of third monolith anion exchanger D)
The third monolith D produced by the above method was cut into a disk shape having an outer diameter of 70 mm and a thickness of about 15 mm. To this, 1400 ml of dimethoxymethane and 20 ml of tin tetrachloride were added, and 560 ml of chlorosulfuric acid was added dropwise under ice cooling. After completion of the dropwise addition, the temperature was raised and reacted at 35 ° C. for 5 hours to introduce a chloromethyl group. After completion of the reaction, the mother liquor was extracted with a siphon, washed with a mixed solvent of THF / water = 2/1, and further washed with THF. To this chloromethylated monolith, 1000 ml of THF and 600 ml of a 30% trimethylamine aqueous solution were added and reacted at 60 ° C. for 6 hours. After completion of the reaction, the product was washed with a methanol / water mixed solvent and then washed with pure water to obtain a third monolith anion exchanger D.

  The resulting third monolith anion exchanger D had a swelling ratio of 1.7 times before and after the introduction of anion exchange groups, and the anion exchange capacity per volume was 0.60 mg equivalent / ml in a wet state. The average diameter of the opening of the monolith anion exchanger in the water wet state was estimated to be 54 μm from the value of the monolith and the swelling ratio of the monolith anion exchanger in the water wet state. Further, the average thickness of the wall part constituting the skeleton of the third monolith anion exchanger D (dried body) obtained by the same method as that of the monolith was 50 μm, the skeleton part area was 28% in the photographic region of the SEM photograph, and in the dry state. The total pore volume of was 2.2 ml / g. The differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.017 MPa / m · LV, which is a lower pressure loss than that required for practical use. It was.

  Next, in order to confirm the distribution state of the quaternary ammonium groups in the third monolith anion exchanger D, the monolith anion exchanger is treated with an aqueous hydrochloric acid solution to form a chloride form, and then the skeleton surface and the skeleton cross section by EPMA. As a result of observation of the distribution state of chloride ions, chloride ions are distributed uniformly not only on the skeleton surface of the monolith anion exchanger but also inside the skeleton, and quaternary ammonium groups are present in the monolith anion exchanger. It was confirmed that it was introduced uniformly.

(Preparation of platinum group metal supported catalyst 5)
A platinum group metal-supported catalyst 5 was obtained in the same manner as in Example 1 except that the third monolith anion exchanger D was used instead of the fourth monolith anion exchanger A. The average particle diameter of the palladium particles supported on the platinum group metal supported catalyst 5 was 4.5 nm, and the degree of uniformity was 2. The supported amount of palladium particles of the platinum group metal supported catalyst 5 was 1.9% by weight in a dry state.

(Example 6)
<Production of platinum group metal supported catalyst 6>
(Step I; production of monolith intermediate (5-1))
19.85 g of styrene, 0.40 g of divinylbenzene, 1.07 g of sorbitan monooleate (hereinafter abbreviated as SMO) and 0.26 g of 2,2′-azobis (isobutyronitrile) were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / SMO / 2,2′-azobis (isobutyronitrile) mixture is added to a mixed solution composed of 1.8 ml of THF and 180 ml of pure water, and vacuum stirring which is a planetary stirring device. The mixture was stirred under reduced pressure in a temperature range of 5 to 20 ° C. using a defoaming mixer (manufactured by EM Corporation) to obtain a water-in-oil emulsion. This emulsion was quickly transferred to a reaction vessel and allowed to polymerize at 60 ° C. for 24 hours in a static state after sealing. After completion of the polymerization, the content was taken out, extracted with methanol, and then dried under reduced pressure to produce a monolith intermediate (5-1) E having a continuous macropore structure and a crosslinking density of 1.3 mol%. The average diameter in the dry state of the opening (mesopore) where the macropores overlap with the macropores of the monolith intermediate (5-1) E measured by the mercury intrusion method is 56 μm, and the total pore volume in the dry state is 7.5 ml. / g.

(Manufacture of 5-1 Monolith E)
Next, 58.8 g of styrene, 1.2 g of divinylbenzene, 150 g of 1-decanol, and 0.5 g of 2,2′-azobis (2,4-dimethylvaleronitrile) were mixed and dissolved uniformly (step II). Next, the monolith intermediate (5-1) E was cut into a disk shape having a diameter of 70 mm and a thickness of about 30 mm to obtain 8.1 g. The separated monolith intermediate (5-1) is placed in a reaction vessel having an inner diameter of 89 mm and immersed in the styrene / divinylbenzene / 1-decanol / 2,2′-azobis (2,4-dimethylvaleronitrile) mixture. After defoaming in a vacuum chamber, the reaction vessel was sealed and allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the monolith-like contents having a thickness of about 60 mm were taken out, subjected to Soxhlet extraction with acetone, and then dried under reduced pressure at 85 ° C. overnight to obtain 5-1 monolith E (step III).

FIG. 9 shows the result of observing the internal structure of the 5-1 monolith E (dry body) containing 1.3 mol% of the cross-linking component composed of the styrene / divinylbenzene copolymer obtained by SEM as described above. Shown in The 5-1 monolith E has a continuous macropore structure, and the surface of the skeleton phase constituting the continuous macropore structure is coated with particles having an average particle diameter of 3 μm, and the particle coverage is 70%. It was. Moreover, the ratio for which the particle body with a particle size of 3-5 micrometers occupied to the whole particle body was 90%. Moreover, the average diameter in the dry state of the opening of the 5-1 monolith E measured by the mercury intrusion method was 27 μm, and the total pore volume in the dry state was 3.1 ml / g.
The change (expansion rate) when the 5-1 monolith E in the dry state was wetted with water was 1.2 times, and the water of the 5-1 monolith E estimated from this expansion rate The average diameter of the openings in the wet state was 32 μm, and the average particle diameter of the particles covering the surface of the skeleton phase was 4 μm.

(Production of 5-1 Monolith Anion Exchanger E)
The 5-1 monolith E produced by the above method was cut into a disk shape having a diameter of 70 mm and a thickness of about 15 mm. To this, 1400 ml of dimethoxymethane and 20 ml of tin tetrachloride were added, and 560 ml of chlorosulfuric acid was added dropwise under ice cooling. After completion of the dropping, the temperature was raised and the reaction was carried out at 35 ° C. for 5 hours to introduce a chloromethyl group. After completion of the reaction, the mother liquor was extracted with a siphon, washed with a mixed solvent of THF / water = 2/1, and further washed with THF. To this chloromethylated monolith, 1000 ml of THF and 600 ml of a 30% trimethylamine aqueous solution were added and reacted at 60 ° C. for 6 hours. After completion of the reaction, the product was washed with a methanol / water mixed solvent and then with pure water to isolate the 5-1 monolith anion exchanger E.

  The swelling ratio before and after introduction of the anion exchange group of the obtained 5-1 monolith anion exchanger E was 1.7 times, and the anion exchange capacity per volume was 0.40 mg equivalent / ml in a wet state with water. . The average diameter of the opening of the 5-1 monolith anion exchanger E in the wet state of water is the value of the 5-1 monolith E and the swelling of the 5-1 monolith anion exchanger E before and after the introduction of the anion exchange group When estimated from the rate, it was 46 μm, and the average particle diameter of the coated particles determined by the same method was 5 μm. In addition, the particle | grain coverage of the skeleton surface by all the particle bodies etc. was 70%, and the ratio for which the particle body of a particle size of 5-8 micrometers occupied in the whole particle body was 90%. The total pore volume in the dry state of the 5-1 monolith anion exchanger E was 3.1 ml / g.

  The differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.012 MPa / m · LV, which is a low pressure loss that does not cause any practical problems.

  Next, in order to confirm the distribution state of the quaternary ammonium group in the 5-1 monolith anion exchanger E, the 5-1 monolith anion exchanger E was treated with an aqueous hydrochloric acid solution to form a chloride form. The distribution of chloride anions on the skeleton surface and skeleton cross section was observed by EPMA. Chloride anions were uniformly distributed not only in the skeleton surface of the monolith anion exchanger but also in the skeleton. Was uniformly introduced into the 5-1 monolith anion exchanger E.

(Preparation of platinum group metal supported catalyst 6)
A platinum group metal-supported catalyst 6 was obtained in the same manner as in Example 1 except that the 5-1 monolith anion exchanger E was used instead of the fourth monolith anion exchanger A. The average particle diameter of the palladium particles supported on the platinum group metal-supported catalyst 6 was 4.2 nm, and the uniformity number was 2. The supported amount of palladium particles of the platinum group metal supported catalyst 6 was 2.1% by weight in a dry state.

(Example 7)
<Manufacture of platinum group metal supported catalyst 7>
(Step I; production of monolith intermediate (5-2))
9.33 g of styrene, 0.14 g of divinylbenzene, 0.50 g of sorbitan monooleate (hereinafter abbreviated as SMO) and 0.26 g of 2,2′-azobis (isobutyronitrile) were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / SMO / 2,2′-azobis (isobutyronitrile) mixture is added to 180 g of pure water, and a vacuum stirring defoaming mixer (manufactured by EM Corp.) which is a planetary stirring device. Was used under reduced pressure in a temperature range of 5 to 20 ° C. to obtain a water-in-oil emulsion. The emulsion was immediately transferred to a reaction vessel, and after sealing, it was allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the content was taken out, extracted with isopropanol, and then dried under reduced pressure to produce a monolith intermediate (5-2) F having a continuous macropore structure and a crosslink density of 1.0 mol%. The average diameter in the dry state of the opening (mesopore) where the macropores of the monolith intermediate (5-2) F overlap each other was 28 μm, and the total pore volume in the dry state was 17.2 ml / g.

(Production of Monolith F of No. 5-2)
39.4 g of vinylbenzyl chloride, 0.6 g of divinylbenzene, 60 g of 1-butanol, and 0.4 g of 2,2′-azobis (2,4-dimethylvaleronitrile) were mixed and dissolved uniformly (step II). The 10-hour half-life temperature of 2,2′-azobis (2,4-dimethylvaleronitrile) used as the polymerization initiator was 51 ° C. The amount of divinylbenzene used relative to the total amount of vinylbenzyl chloride and divinylbenzene used in Step II was 1.4 mol%, relative to the crosslink density of 1.0 mol% of monolith intermediate (5-2) F. . Next, the monolith intermediate (5-2) F was cut into a disk shape having an outer diameter of 70 mm and a thickness of about 20 mm, and 2.9 g was obtained. The separated monolith intermediate (5-2) F is placed in a reaction vessel having an inner diameter of 73 mm and immersed in the styrene / divinylbenzene / 1-butanol / 2,2′-azobis (2,4-dimethylvaleronitrile) mixture. After defoaming in a vacuum chamber, the reaction vessel was sealed and allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the monolith-like contents having a thickness of about 30 mm were taken out, subjected to Soxhlet extraction with acetone, and then dried under reduced pressure at 85 ° C. overnight to obtain No. 5-2 monolith F (step III).

  The internal structure of the 5-2 monolith F (dried product) made of the vinylbenzyl chloride / divinylbenzene copolymer thus obtained was observed by SEM. The 5-2 monolith F was co-continuous. The surface of the skeletal phase that has a structure and constitutes the co-continuous structure was coated with particles having an average particle diameter of 10 μm, and the particle coverage by all particles was 100%. Moreover, the ratio for which the particle body with a particle size of 6-12 micrometers occupied to the whole particle body was 80%.

Moreover, the average diameter in the dry state of the opening (hole) of the 5-2 monolith F measured by mercury porosimetry was 29 μm, and the total pore volume in the dry state was 2.1 ml / g.
The change (expansion coefficient) when the dried monolith F-2 is wet with water is 1.2 times, and the water of the 5-2 monolith F estimated from this expansion coefficient is 1.2 times. The average diameter of the openings (holes) in the wet state was 34 μm, and the average particle diameter of the particles covering the surface of the skeletal phase was 12 μm.

(Production of Monolith Anion Exchanger F of No. 5-2)
The 5-2 monolith F manufactured by the above method was cut into a disk shape having an outer diameter of 70 mm and a thickness of about 15 mm. The weight of the 5-2 monolith F was 17.9 g. To this was added 1500 ml of tetrahydrofuran, heated at 40 ° C. for 1 hour, cooled to 10 ° C. or lower, gradually added 114.5 g of a 30% trimethylamine aqueous solution, heated to react at 40 ° C. for 24 hours. After completion of the reaction, the mixture was washed with methanol to remove tetrahydrofuran, and further washed with pure water to obtain a 5-2 monolith anion exchanger F.

  The swelling ratio of the obtained 5-2 monolith anion exchanger F before and after introduction of the anion exchange group was 2.0 times, and the anion exchange capacity per volume was 0.32 mg equivalent / ml in a wet state. It was. The average diameter of the continuous pores of the 5-2 monolith anion exchanger F in the water-wet state is the value of the 5-2 monolith F and the 5-2 monolith anion exchanger F before and after introduction of the anion exchange group. The average diameter of the protrusions determined by the same method was 20 μm and the particle coverage was 100%. The total pore volume in the dry state of the 5-2 monolith anion exchanger F was 2.1 ml / g. The differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.041 MPa / m · LV, which is a lower pressure loss than that required for practical use. It was. Moreover, the ratio for which the particle body with a particle size of 12-24 micrometers occupied to the whole particle body was 80%.

  Next, in order to confirm the distribution state of the quaternary ammonium group in the 5-2 monolith anion exchanger F, after treating the 5-2 monolith anion exchanger with an aqueous hydrochloric acid solution into a chloride form, When the distribution state of the chloride anion on the skeleton surface and the skeleton cross section was observed by EPMA, the chloride anion was uniformly distributed not only in the skeleton surface of the 5-2 monolith anion exchanger F but also in the skeleton. It was confirmed that quaternary ammonium groups were uniformly introduced into the 5-2 monolith anion exchanger.

(Preparation of platinum group metal supported catalyst 7)
A platinum group metal supported catalyst 7 was obtained in the same manner as in Example 1 except that the 5-2 monolith anion exchanger F was used instead of the fourth monolith anion exchanger A. The average particle diameter of the palladium particles supported on the platinum group metal supported catalyst 7 was 4.1 nm, and the degree of uniformity was 2. The supported amount of palladium particles of the platinum group metal supported catalyst 7 was 2.0% by weight in a dry state.

(Example 8)
<Manufacture of platinum group metal supported catalyst 8>
(Step I; production of monolith intermediate (6))
19.9 g of styrene, 0.4 g of divinylbenzene, 1.1 g of sorbitan monooleate (hereinafter abbreviated as SMO) and 0.26 g of 2,2′-azobis (isobutyronitrile) were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / SMO / 2,2′-azobis (isobutyronitrile) mixture is added to a mixed solution composed of 1.8 ml of THF and 180 ml of pure water, and vacuum stirring which is a planetary stirring device. The mixture was stirred under reduced pressure in a temperature range of 5 to 20 ° C. using a defoaming mixer (manufactured by EM Corporation) to obtain a water-in-oil emulsion. This emulsion was quickly transferred to a reaction vessel and allowed to polymerize at 60 ° C. for 24 hours in a static state after sealing. After completion of the polymerization, the content was taken out, extracted with methanol, and then dried under reduced pressure to produce a monolith intermediate (6) G having a continuous macropore structure and a crosslinking density of 1.3 mol%. The average diameter in the dry state of the opening (mesopore) of the portion where the macropores and macropores of the monolith intermediate (6) G measured by mercury porosimetry is 56 μm, and the total pore volume in the dry state is 7.5 ml / g. Met.

(Production of sixth monolith G)
Next, 59.4 g of styrene, 0.6 g of divinylbenzene, 50 g of 1-octanol, 0.5 g of 2,2′-azobis (2,4-dimethylvaleronitrile) were mixed and dissolved uniformly (step II). Next, the monolith intermediate (6) G was cut into a disk shape having a diameter of 70 mm and a thickness of about 30 mm to obtain 7.7 g. The separated monolith intermediate (6) G is put in a reaction vessel having an inner diameter of 89 mm, immersed in the styrene / divinylbenzene / 1-octanol / 2,2′-azobis (2,4-dimethylvaleronitrile) mixture, and the pressure is reduced. After defoaming in the chamber, the reaction vessel was sealed and allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the monolith-like contents having a thickness of about 60 mm were taken out, soxhlet extracted with acetone, and then dried under reduced pressure at 85 ° C. overnight to obtain a sixth monolith G (step III).

FIG. 11 shows the result of observing the internal structure of the sixth monolith G (dried product) containing 0.6 mol% of the crosslinking component made of the styrene / divinylbenzene copolymer obtained by SEM as described above. . The sixth monolith G has a continuous macropore structure, and a honeycomb-like porous structure was also introduced into the skeleton part constituting the continuous macropore structure. The average diameter in the dry state of the opening of the sixth monolith G measured by the mercury intrusion method is 35 μm, the total pore volume in the dry state is 1.7 ml / g, and the specific surface area in the dry state is 55.2 m ^2. / g.
In addition, the change (expansion rate) when the sixth monolith G in the dry state was wetted with water was 1.3 times, and the sixth monolith G in the water wet state estimated from this expansion rate was obtained. The average diameter of the openings was 46 μm.

(Production of sixth monolith anion exchanger G)
The sixth monolith G manufactured by the above method was cut into a disk shape having a diameter of 70 mm and a thickness of about 15 mm. To this, 1400 ml of dimethoxymethane and 40 ml of tin tetrachloride were added, and 560 ml of chlorosulfuric acid was added dropwise under ice cooling. After completion of the dropping, the temperature was raised and the reaction was carried out at 35 ° C. for 5 hours to introduce a chloromethyl group. After completion of the reaction, the mother liquor was extracted with a siphon, washed with a mixed solvent of THF / water = 2/1, and further washed with THF. To this chloromethylated monolith, 1000 ml of THF and 600 ml of a 30% trimethylamine aqueous solution were added and reacted at 60 ° C. for 6 hours. After completion of the reaction, the product was washed with a methanol / water mixed solvent and then washed with pure water to obtain a sixth monolith anion exchanger G.

The swelling ratio of the obtained sixth monolith anion exchanger G before and after the introduction of anion exchange groups was 1.5 times, and the anion exchange capacity per volume was 0.75 mg equivalent / ml in a water-wet state. The average diameter of the openings of the sixth monolith anion exchanger G in the water-wet state was estimated from the value of the sixth monolith G and the swelling ratio of the sixth monolith anion exchanger G before and after the introduction of the anion exchange group. Met. The total pore volume in the dry state of the sixth monolith anion exchanger G was 1.7 ml / g, and the specific surface area was 55.2 m ² / g.

  Next, in order to confirm the distribution state of the quaternary ammonium groups in the sixth monolith anion exchanger G, the sixth monolith anion exchanger G is treated with an aqueous hydrochloric acid solution to form a chloride form, and then the skeleton is formed by EPMA. Observation of the distribution state of chloride anions on the surface and the cross section of the skeleton revealed that the chloride anions were uniformly distributed not only on the skeleton surface of the sixth monolith anion exchanger G but also inside the skeleton. It was confirmed that was uniformly introduced into the monolith anion exchanger.

  The differential pressure coefficient, which is an index of the pressure loss when water is permeated, is 0.016 MPa / m · LV, which is a low pressure loss that has no practical problem.

(Preparation of platinum group metal supported catalyst 8)
A platinum group metal supported catalyst 8 was obtained in the same manner as in Example 1, except that the sixth monolith anion exchanger G was used instead of the fourth monolith anion exchanger A. The average particle diameter of the palladium particles supported on the platinum group metal supported catalyst 8 was 4.4 nm, and the degree of uniformity was 2. Further, the supported amount of palladium particles of the platinum group metal supported catalyst 8 was 2.4% by weight in a dry state.

(Examples 9 to 15)
(Preparation of platinum group metal supported catalysts 9 to 15)
As shown in Table 5, the fourth monolith A manufactured in Example 1, the first monolith B manufactured in Example 3, the second monolith C manufactured in Example 4, and the first monolith C manufactured in Example 5. 3 monolith D, the 5-1 monolith E produced in Example 6, the 5-2 monolith F produced in Example 7, and the sixth monolith G produced in Example 8 were swollen in water. Was cut into a cylindrical shape having a diameter of 30 mm and a thickness of 15 mm.
Next, the water-swelled monolith and 5 ml of the palladium nanocolloid solution (4% by weight of palladium) used in Example 1 were placed in a pressure vessel and sealed. The sealed pressure vessel was placed in a constant temperature bath at 40 ° C. Carbon dioxide was introduced into the pressure vessel until it reached 25 MPa. The introduction was stopped when the pressure reached 25 MPa, and the state was maintained for 1 hour. After 1 hour, the pressure vessel was opened to release carbon dioxide. The monolith carrying palladium was taken out from the pressure vessel, and platinum group metal supported catalysts 9 to 15 were obtained.
Table 5 shows the average particle diameter, the degree of uniformity, and the amount supported in the dry state of the palladium particles supported on the obtained platinum group metal supported catalyst.

DESCRIPTION OF SYMBOLS 1 Skeletal phase 2 Pore phase 10 Monolith 11 Image area 12 Skeletal part 13 shown in cross section Macropore 21 Skeletal surface 22 Projection body 30 Monolith (monolith ion exchanger)
31 Macropore 32 Opening 33 Inner layer portion 34 Surface layer portion 35 Gas phase portion (bubble portion)
36 Wall (skeleton)
37 pores

Claims (8)

  A platinum group metal-supported catalyst in which platinum group metal particles having an average particle diameter of 1 to 100 nm are supported on a monolithic organic porous body or a monolithic organic porous ion exchanger, and the degree of uniformity of the platinum group metal particles Is a platinum group metal supported catalyst, wherein the supported amount of the platinum group metal particles is 0.004 to 20% by weight in a dry state.   The supported platinum group metal catalyst according to claim 1, wherein the supported amount of the platinum group metal particles is 0.004 to 2.0 wt%.   By contacting the monolithic organic porous material or the monolithic organic porous ion exchanger with a fluid containing platinum group metal particles having an average particle diameter of 1 to 100 nm and a homogeneity of 10 or less, the monolithic shape is obtained. A platinum group metal-supported catalyst comprising a platinum group metal-supported step of obtaining a platinum group metal-supported catalyst by supporting the platinum group metal particles on an organic porous material or the monolithic organic porous ion exchanger. Production method.   4. The method for producing a platinum group metal-supported catalyst according to claim 3, wherein the fluid containing the platinum group metal particles is a supercritical fluid containing platinum group metal particles.   The platinum group metal-supported catalyst according to claim 1 or 2 is brought into contact with water to be treated containing hydrogen peroxide to decompose and remove the hydrogen peroxide in the water to be treated containing hydrogen peroxide. A method for producing hydrogen peroxide decomposition-treated water. 6. The method for producing hydrogen peroxide decomposition treated water according to claim 5, wherein the water to be treated containing hydrogen peroxide is brought into contact with the platinum group metal supported catalyst at SV = 2000 to 40000h- ^1. .   The oxygen-containing catalyst is produced by reacting dissolved oxygen and hydrogen in the water to be treated containing oxygen in the presence of the platinum group metal supported catalyst according to claim 1 or 2 to produce water. A method for producing treated water for removing dissolved oxygen, characterized in that dissolved oxygen is removed from the treated water. The method for producing dissolved oxygen-removed treated water according to claim 7, wherein the water to be treated containing oxygen is brought into contact with the platinum group metal-supported catalyst at SV = 2000 to 40000 h ⁻¹ .

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