JP5048712B2 - Electric deionized water production equipment - Google Patents

Description

  The present invention relates to the production of electric deionized water used in various industries such as semiconductor manufacturing industry, pharmaceutical industry, food industry, power plant, laboratory, etc. using deionized water, or the production of sugar liquid, juice, wine, etc. It relates to the device.

  As a method for producing deionized water, there is conventionally known a method of deionizing granular ion exchange resin (hereinafter, also simply referred to as “ion exchange resin”) through treated water. In this method, ion exchange resin is used. When the ion exchange capacity of the product decreases, it is necessary to regenerate with chemicals. To eliminate such disadvantages in processing operations, there is a method for producing deionized water by electric deionization that does not require any chemical regeneration. Established and put into practical use.

  In Japanese Patent Application Laid-Open No. 2006-15260, a DC electric field is applied to a deionization chamber filled with an ion exchanger so that ions to be excluded migrate in the same direction or in the opposite direction with respect to the direction of water flow in the ion exchanger. In the electric deionized water production apparatus that excludes ionic impurities adsorbed on the ion exchanger out of the system, the ion exchanger is composed of a monolithic organic porous ion exchanger and a granular ion exchange resin. A monolithic organic porous ion exchanger having an open-cell structure with macropores connected to each other and mesopores with an average diameter of 1-1000 μm in the walls of the macropores, and a total pore volume of 1 ml Disclosed is an electric deionized water production apparatus in which the ion exchange groups are uniformly distributed and the ion exchange capacity is 0.5 mg equivalent / g or more of a dry porous body. It has been. The details of the method for producing a monolithic organic porous ion exchanger used in this electric deionized water production apparatus are disclosed in JP-A-2002-306976.

  According to the electric deionized water production apparatus disclosed in Japanese Patent Application Laid-Open No. 2006-15260, the monolith is used as part of the ion exchanger filled in the deion exchange chamber. Can be buffered by the physical stretchability of the monolith, and the filling state in the deionization chamber can be kept uniform. In addition, since it can prevent swelling and shrinkage due to ion exchange reaction and poor contact with ion exchange membrane, simplified deion exchange chamber structure with wide space that could not be achieved with a single ion exchange resin Can reduce the material cost, processing cost, and assembly cost. In addition, compared to ion exchange resins, monoliths have a faster ion movement speed and shorter ion exchanger lengths, so monoliths placed near the treated water inlet facilitate the discharge of ions and treat high-ion concentration water. The monolith arranged in the vicinity of the treated water outlet can suppress the leakage of a trace amount of ions in a dilute concentration region and obtain high-purity treated water. Also, by placing a monolith near the treated water inlet of the deionization chamber, the removal rate of hardness components such as calcium is improved in the decation chamber, and anions such as carbonic acid and silica are eliminated in the deionization chamber. Increases speed.

JP 2006-15260 A JP 2002-306976 A JP 2009-62512 A JP 2009-67982 A

  However, the organic porous ion exchangers described in JP-A-2006-15260 and JP-A-2002-306976 have a common monolithic opening (mesopore) of 1 to 1,000 μm, For monoliths with a small pore volume of 5 ml / g or less in pore volume, it is necessary to reduce the amount of water droplets in the water-in-oil emulsion, so the common aperture is small, and the average diameter of the aperture is substantially 20 μm or more. Cannot be manufactured. For this reason, there existed a problem that the pressure loss at the time of water flow was large. In addition, when the average diameter of the openings is around 20 μm, the total pore volume also increases accordingly, so that the ion exchange capacity per volume decreases, and thus the quality of treated water and the power consumption increase. There was a problem. In addition, in the monolith loaded in the demineralization chamber of the electric deionized water production apparatus, the appearance of a monolith having a new structure different from the open cell structure (continuous macropore) has been desired.

  Therefore, the object of the present invention is to maintain the advantages of the mixed ion exchanger of the monolith and the granular ion exchange resin filled in the horizontal desalting chamber of JP-A-2006-15260, while the strength of the ion exchanger is high, An object of the present invention is to provide an electric deionized water production apparatus that can reduce pressure loss during water flow, has good treated water quality, and has low power consumption.

  Under such circumstances, the present inventors have conducted intensive studies, and as a result, obtained a monolithic organic porous body (intermediate) having a relatively large pore volume obtained by the method described in JP-A-2003-334560. If the vinyl monomer and the crosslinking agent are allowed to stand and polymerize in an organic solvent under specific conditions in the presence, a large number of particles having a diameter of 2 to 20 μm are fixed on the surface of the skeleton constituting the organic porous body, or a protrusion. When a monolith having a composite structure in which is formed, a composite monolith ion exchanger in which an ion exchange group is introduced into the composite monolith is used as a part of a mixed ion exchanger of an electric deionized water production apparatus, The movement of adsorbed ionic impurities is accelerated to facilitate the removal of adsorbed ions, the strength of the ion exchanger is high, the pressure loss during water flow can be reduced, the quality of treated water is good, and Expenses found such that the power is low, which resulted in the completion of the present invention.

  That is, the present invention applies a DC electric field to a deionization chamber filled with an ion exchanger so that ions to be excluded migrate in the same direction or in the opposite direction to the direction of water flow in the ion exchanger. In the electric deionized water production apparatus for removing ionic impurities adsorbed on the ion exchanger out of the system, the ion exchanger is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin. Thus, the monolithic organic porous ion exchanger comprises 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, or A composite structure of a large number of protrusions having a size of 4 to 40 μm formed on the skeleton surface of the organic porous body, and having an average pore diameter of 10 to 150 μm and a total pore volume of 0 in a wet state of water. .5-5ml / g , There is provided an electrodeionization water producing apparatus, characterized in that per volume of water wet state is ion exchange capacity 0.2mg equivalent / ml or more.

  The present invention also includes a deanion chamber partitioned by an anion exchange membrane on one side and an ion exchange membrane on the other side, an anode disposed outside the anion exchange membrane on the one side, and the other side A cathode disposed outside the ion exchange membrane, supplying water to be treated from the vicinity of the anion exchange membrane on one side in the deanion ion chamber, and ions on the other side in the deanion ion chamber An anion cell that obtains the first treated water from the vicinity of the exchange membrane, a decation chamber that is partitioned by the cation exchange membrane on one side and the ion exchange membrane on the other side, and disposed outside the cation exchange membrane on the one side And an anode disposed outside the ion exchange membrane on the other side, and supplying the first treated water of the anion cell from the vicinity of the cation exchange membrane on one side in the decation chamber. And a cation cell for obtaining the second treated water from the vicinity of the ion exchange membrane on the other side in the decation chamber. Among the ion exchangers filled in the deanion chamber and decation chamber, at least one is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous An organic porous body in which an ion exchanger is composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or a skeleton surface of the organic porous body It is a composite structure with a large number of protrusions having a size of 4 to 40 μm formed on the surface, and has an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state. The present invention provides an apparatus for producing electric deionized water having an ion exchange capacity per volume of 0.2 mg equivalent / ml or more in a wet state of water.

  The present invention also provides a decation chamber partitioned by a cation exchange membrane on one side and an ion exchange membrane on the other side, a cathode disposed outside the cation exchange membrane on the one side, and the other side Having an anode disposed outside the ion exchange membrane, supplying water to be treated from the vicinity of one cation exchange membrane in the decation chamber, and performing ion exchange on the other side in the decation chamber A cation cell for obtaining first treated water from the vicinity of the membrane, a deanion chamber partitioned by an anion exchange membrane on one side and an ion exchange membrane on the other side, and an outer side of the anion exchange membrane on the one side A cathode disposed outside the ion exchange membrane on the other side, and supplying the first treated water of the cation cell from the vicinity of the anion exchange membrane on one side in the deanion chamber. And an anion cell for obtaining the second treated water from the vicinity of the ion exchange membrane on the other side in the deanion ion chamber, At least one of the ion exchangers filled in the decation chamber and the deanion chamber is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, and the monolithic organic porous ion The exchanger is an organic porous body composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or the skeleton surface of the organic porous body A composite structure with a large number of protrusions having a size of 4 to 40 μm, and having an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state, It is an object of the present invention to provide an electric deionized water production apparatus having an ion exchange capacity of 0.2 mg equivalent / ml or more per volume in a water wet state.

  In addition, the present invention provides a detachment method in which an intermediate ion exchange membrane is provided between an anion exchange membrane on one side and a cation exchange membrane on the other side, and is partitioned by the anion exchange membrane on the one side and the intermediate ion exchange membrane. A decation chamber partitioned by the anion chamber, the cation exchange membrane on the other side and the intermediate ion exchange membrane; an anode outside the anion exchange membrane on the one side; and a cation on the other side A deionization cell in which a cathode is disposed outside an exchange membrane, wherein water to be treated is supplied from the vicinity of the other cation exchange membrane in the decation chamber and intermediate ions in the decation chamber First treated water is obtained from the vicinity of the exchange membrane, and the first treated water is supplied from the vicinity of the anion exchange membrane on one side of the deanion chamber, and from the vicinity of the intermediate ion exchange membrane in the deanion chamber. A second treated water is obtained in an ion exchanger filled in the deanion chamber and decation chamber. At least one is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous ion exchanger comprising an organic porous body composed of a continuous skeleton phase and a continuous pore phase; , A composite structure with a large number of particles having a diameter of 4 to 40 μm fixed on the skeleton surface of the organic 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 body has an average pore diameter of 10 to 150 μm in a water-wet state, a total pore volume of 0.5 to 5 ml / g, and an ion exchange capacity per volume in a water-wet state of 0.2 mg equivalent / ml or more. An electrical deionized water production apparatus is provided.

  In addition, the present invention provides a desorption method in which an intermediate ion exchange membrane is provided between a cation exchange membrane on one side and an anion exchange membrane on the other side, and is partitioned by the cation exchange membrane on the one side and the intermediate ion exchange membrane. A deionization chamber defined by a cation chamber, the other side anion exchange membrane and the intermediate ion exchange membrane; a cathode outside the one side cation exchange membrane; and an anion on the other side A deionization cell in which an anode is disposed outside an exchange membrane, wherein water to be treated is supplied from the vicinity of the anion exchange membrane on the other side in the deionization chamber, and intermediate ions in the deionization chamber First treated water is obtained from the vicinity of the exchange membrane, and the first treated water is supplied from the vicinity of one cation exchange membrane in the decation chamber, and from the vicinity of the intermediate ion exchange membrane in the decation chamber. A second treated water is obtained in an ion exchanger filled in the decation chamber and deion chamber. At least one is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous ion exchanger comprising an organic porous body composed of a continuous skeleton phase and a continuous pore phase; , A composite structure with a large number of particles having a diameter of 4 to 40 μm fixed on the skeleton surface of the organic 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 body has an average pore diameter of 10 to 150 μm in a water-wet state, a total pore volume of 0.5 to 5 ml / g, and an ion exchange capacity per volume in a water-wet state of 0.2 mg equivalent / ml or more. An electrical deionized water production apparatus is provided.

  The present invention also includes a deionization chamber partitioned by an anion exchange membrane on one side and a cation exchange membrane on the other side, an anode disposed outside the anion exchange membrane on the one side, and the other side A cathode disposed outside the cation exchange membrane, supplying water to be treated from the vicinity of the anion exchange membrane on one side in the deionization chamber, and cation on the other side in the deionization chamber Treated water is obtained from the vicinity of the exchange membrane, or treated water is supplied from the vicinity of the other cation exchange membrane in the deionization chamber and treated from the vicinity of the anion exchange membrane on one side of the deionization chamber. The ion exchanger filled with the deionization chamber is a monolithic organic porous anion exchanger, a granular anion exchange resin phase and a monolithic organic porous from the anode side to the cathode side. It is a layered body in which cation exchangers are laminated, or particulate anion exchange resin compatibility A layered body in which monolithic organic porous cation exchangers are laminated, wherein the monolithic organic porous anion exchanger and the monolithic organic porous cation exchanger are composed of a continuous skeleton phase and a continuous pore phase. A porous body and a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic 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 And having an average pore diameter of 10 to 150 μm in a water-wet state, a total pore volume of 0.5 to 5 ml / g, and an ion exchange capacity of 0.2 mg equivalent per volume in the water-wet state The present invention provides an electric deionized water production apparatus having a capacity of at least / ml.

  According to the present invention, the strength of the ion exchanger is high while maintaining the advantages of the mixed ion exchanger of the monolith and the granular ion exchange resin filled in the horizontal desalting chamber of Japanese Patent Application Laid-Open No. 2006-15260. The pressure loss at the time can be reduced, the quality of the treated water is good, and the power consumption is small. That is, compared to the monolith described in Japanese Patent Application Laid-Open No. 2006-15260, since the ion moving speed is high and the ion exchanger length is short, the monolith arranged in the vicinity of the to-be-treated water inlet promotes the discharge of ions to increase the high ion The monolith which enables treatment of concentrated water and is disposed in the vicinity of the treated water outlet can suppress the leakage of a trace amount of ions in a dilute concentration region and obtain high-purity treated water.

4 is a SEM image of a monolith obtained in Reference Example 1 at a magnification of 100. FIG. 3 is a SEM image of a monolith obtained in Reference Example 1 at a magnification of 300. 3 is an SEM image of the monolith obtained in Reference Example 1 at a magnification of 3000. 2 is an EPMA image showing the distribution state of sulfur atoms on the surface of the monolith cation exchanger obtained in Reference Example 1. FIG. 2 is an EPMA image showing a distribution state of sulfur atoms in the cross-section (thickness) direction of the monolith cation exchanger obtained in Reference Example 1. FIG. 10 is a SEM image of a monolith obtained in Reference Example 2 at a magnification of 100. 6 is an SEM image of a monolith obtained in Reference Example 2 at a magnification of 600. 4 is an SEM image of the monolith obtained in Reference Example 2 at a magnification of 3000. 10 is an SEM image of a monolith obtained in Reference Example 3 at a magnification of 600. 10 is an SEM image of the monolith obtained in Reference Example 3 at a magnification of 3000. 10 is a SEM image of the monolith obtained in Reference Example 4 at a magnification of 3000. 10 is an SEM image of a monolith obtained in Reference Example 5 at a magnification of 100. 10 is a SEM image of the monolith obtained in Reference Example 5 at a magnification of 3000. 10 is a SEM image of a monolith obtained in Reference Example 6 at a magnification of 100. 10 is an SEM image of a monolith obtained in Reference Example 6 at a magnification of 600. 10 is an SEM image of the monolith obtained in Reference Example 6 at a magnification of 3000. It is a figure explaining the swelling and shrinkage | contraction of a monolith-ion exchange resin mixture. It is a schematic diagram which shows the structure of the electrical deionized water manufacturing apparatus of the 1st Example of this invention. It is a schematic diagram which shows the structure of the electrical deionized water manufacturing apparatus of the 2nd Example of this invention. It is a schematic diagram which shows the structure of the electrical deionized water manufacturing apparatus of the 3rd Example of this invention. It is a schematic diagram of the electric decation water production apparatus used in the Example. It is typical sectional drawing of a protrusion.

  The basic structure of the electric deionized water production apparatus of the present invention is to form a deionization chamber by filling a deionization chamber partitioned by ion exchange membranes on both sides with a mixture of a monolith and an ion exchange resin. An electrode for applying a DC electric field is arranged outside the membrane, and the application of the DC electric field is performed so that ions to be eliminated migrate in the same direction or in the opposite direction to the direction of water flow in the ion exchanger. It is. The term “migrate in the same or reverse direction” includes the case of migrating in both the same and reverse directions. In the present invention, the direction of water flow in the mixed ion exchanger refers to the direction of water flow in the substantially central portion of the mixed ion exchanger. For example, as shown in FIG. 14, the treated water inlet and the treated water outlet are substantially diagonal in a side view, and the flow in the mixed ion exchanger is not unidirectional, that is, in the figure, it is not the left-right direction. The water flow direction in the majority of the mixed ion exchanger is generally the left-right direction, and includes such a water flow form. In addition, although it is not necessary to arrange | position a to-be-processed water introduction distribution part and a treated water collection part separately in this mixed ion exchanger, you may install.

  One monolithic organic porous ion exchanger of the mixture filled in the so-called horizontal desalting chamber of the present invention is a monolithic organic porous ion exchanger having a composite structure. In this specification, “monolithic organic porous body” is simply “composite monolith”, “monolithic organic porous ion exchanger” is simply “composite monolithic ion exchanger”, and “monolithic organic porous intermediate”. "Body" is also simply called "monolith intermediate".

<Description of composite monolith ion exchanger>
A composite monolith ion exchanger is obtained by introducing an ion exchange group into a composite monolith, and is fixed to an organic porous body composed of a continuous skeleton phase and a continuous pore phase, and the skeleton surface of the organic porous body. An organic porous body consisting of a continuous skeleton phase and a continuous pore phase, and a size formed on the skeleton surface of the organic porous body. Is a composite structure with a large number of protrusions having a thickness of 4 to 40 μm, and has an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state. The ion exchange capacity per volume is 0.2 mg equivalent / ml or more, and the ion exchange groups are uniformly distributed in the composite structure. In the present specification, “particle bodies” and “projections” may be collectively referred to as “particle bodies”.

  The continuous skeleton phase and the continuous pore phase (dried body) of the organic porous body can be observed by an SEM image. Examples of the basic structure of the organic porous material include a continuous macropore structure and a co-continuous structure. The skeletal phase of the organic porous material appears as a columnar continuum, a concave wall continuum, or a composite thereof, and has a shape that is clearly different from a particle shape or a protrusion shape.

  As a preferable structure of the organic porous material, a continuous macropore structure (hereinafter referred to as “first organic porous ion”) in which bubble-shaped macropores overlap each other and the overlapping portion becomes an opening having an average diameter of 30 to 150 μm in a wet state. And a three-dimensional continuous skeleton with an average thickness of 1 to 60 μm in a water-filled state, and a three-dimensional continuous with an average diameter of 10 to 100 μm in a water-filled state between the skeletons. A co-continuous structure (hereinafter, also referred to as “second organic porous ion exchanger”).

  In the case of the first organic porous ion exchanger, the organic porous body is a continuous macropore structure in which bubble-shaped macropores overlap each other, and the overlapping portion forms an opening (mesopore) having an average diameter of 30 to 150 μm in a water-filled state. It is. The average diameter of the opening of the composite monolith ion exchanger is larger than the average diameter of the opening of the composite monolith in a dry state because the entire composite monolith swells when an ion exchange group is introduced into the monolith. If the average diameter of the openings is less than 30 μm, the pressure loss at the time of water flow is increased, which is not preferable. If the average diameter of the openings is too large, contact between the fluid and the monolith ion exchanger becomes insufficient. As a result, the ion exchange characteristics deteriorate, which is not preferable.

  In the present invention, the average diameter of the openings of the dry monolith intermediate, the average diameter of the pores or openings of the dry composite monolith, and the average diameter of the holes or openings of the dry composite monolith ion exchanger are: It is a value measured by the mercury intrusion method. In the present invention, the average diameter of the pores or openings of the composite monolith ion exchanger in the water state is calculated by multiplying the average diameter of the pores or openings of the composite monolith ion exchanger in the dry state by the swelling rate. Value. Specifically, the diameter of the composite monolith ion exchanger in the water state is x1 (mm), and the diameter of the composite monolith ion exchanger in the dry state obtained by drying the water-soluble composite monolith ion exchanger. Y1 (mm), and when the average diameter of the pores or openings when the dry monolithic ion exchanger is measured by the mercury intrusion method is z1 (μm), the monolithic monolithic ion in the water state The average diameter (μm) of the holes or openings of the exchanger is calculated by the following formula: “Average diameter of holes or openings of the composite monolith ion exchanger in the water state (μm) = z1 × (x1 / y1)” The In addition, the average diameter of the pores or openings of the dry composite monolith before the introduction of the ion exchange group, and the composite monolith ion in the water state relative to the dry composite monolith when the ion exchange group is introduced into the dry composite monolith When the swelling ratio of the exchanger is known, the average diameter of the pores or openings of the composite monolith in the dry state is multiplied by the swelling ratio to calculate the average diameter of the water state of the pores of the composite monolith ion exchanger. You can also.

  In the case of the second organic porous body ion exchanger, the organic porous body has a three-dimensional continuous skeleton with an average diameter of 1 to 60 μm in a water-filled state, and an average diameter between the skeletons in a water-filled state. It is a co-continuous structure having three-dimensionally continuous pores of 10 to 100 μm. If the diameter of the three-dimensionally continuous pores is less than 10 μm, the pressure loss at the time of fluid permeation increases, which is not preferable. If it exceeds 100 μm, the contact between the water to be treated and the organic porous ion exchanger Becomes unsatisfactory, and as a result, the ion exchange characteristics become non-uniform.

  The average diameter of the co-continuous structure pores in the water-filled state is a value calculated by multiplying the average diameter of the pores of the composite monolith ion exchanger in the dry state measured by a known mercury intrusion method and the swelling ratio. It is. Specifically, the diameter of the composite monolith ion exchanger in the water state is x2 (mm), and the diameter of the composite monolith ion exchanger in the dry state obtained by drying the water-soluble composite monolith ion exchanger. Is y2 (mm), and the average diameter of the pores when the dried monolithic ion exchanger is measured by mercury porosimetry is z2 (μm), the pores of the composite monolith ion exchanger The average diameter (μm) in the water state is calculated by the following formula: “average diameter (μm) of water state in the pores of the composite monolith ion exchanger = z2 × (x2 / y2)”. In addition, the average diameter of the pores of the composite monolith in the dry state before the introduction of the ion exchange group, and the composite monolith ion exchanger in the water state relative to the dry composite monolith when the ion exchange group is introduced into the composite monolith in the dry state Can be calculated by multiplying the average diameter of the pores of the composite monolith in the dry state by the swelling ratio. Further, the average thickness of the skeleton of the co-continuous structure in the water state is obtained by performing SEM observation of the composite monolith ion exchanger in the dry state at least three times and measuring the thickness of the skeleton in the obtained image. The average value is calculated by multiplying the swelling ratio. Specifically, the diameter of the composite monolith ion exchanger in the water state is x3 (mm), the diameter of the composite monolith ion exchanger in the dry state obtained by drying the water-soluble composite monolith ion exchanger. Y3 (mm), SEM observation of this dried composite monolith ion exchanger was performed at least three times, the thickness of the skeleton in the obtained image was measured, and the average value was z3 (μm). For example, the average thickness (μm) of the skeleton of the continuous structure of the composite monolith ion exchanger in the water state is expressed by the following formula: “average thickness of the hydrated state of the skeleton of the continuous structure of the composite monolith ion exchanger” (Μm) = z3 × (x3 / y3) ”. In addition, the average thickness of the skeleton of the dry composite monolith before introduction of the ion exchange groups, and the water-soluble composite monolith ion exchanger when the ion exchange groups are introduced into the dry composite monolith. Can be calculated by multiplying the average thickness of the skeleton of the composite monolith in the dry state by the swell ratio, and calculating the average thickness of the hydrated state of the skeleton of the composite monolith ion exchanger. The skeleton forming the co-continuous structure is rod-shaped and has a circular cross-sectional shape, but may have a cross-section with different diameters such as an elliptical cross-sectional shape. The thickness in this case is the average of the minor axis and the major axis.

  Further, if the average diameter of the three-dimensionally continuous skeleton is less than 1 μm, it is not preferable because the ion exchange capacity per volume decreases, and if it exceeds 60 μm, the uniformity of deionization characteristics is lost. Absent.

  A preferable value of the average diameter of the pores of the composite monolith ion exchanger in a wet state with water is 10 to 120 μm. When the organic porous body constituting the composite monolith ion exchanger is the first organic porous body, the preferred pore diameter of the composite monolith ion exchanger is 30 to 120 μm, and the organic porous body constituting the composite monolith ion exchanger In the case of the second organic porous body, a preferable value of the pore diameter of the composite monolith ion exchanger is 10 to 90 μm.

  In the composite monolith ion exchanger according to the present invention, 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. 22 shows a schematic cross-sectional view of the protrusion. As shown in (A) to (E) in FIG. 22, the protrusions protruding from the skeleton surface 61 are the protrusions 62, and the protrusions 62 are like the protrusions 62 a shown in (A). The shape close to a granular shape, a hemispherical shape like a projection 62b shown in (B), and a swell of the skeleton surface like a projection 62c shown in (C). In addition, the protrusion 61 has a shape that is longer in the direction perpendicular to the skeleton surface 61 than in the plane direction of the skeleton surface 61, like the protrusion 62d shown in FIG. There is a thing of the shape which protruded in the several direction like the protrusion 62e 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.

  In the composite monolith ion exchanger according to the present invention, the proportion of 4 to 40 μm particles in a wet state in water 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. The coverage ratio of the surface of the skeleton layer with particles or the like refers to the area ratio on the SEM image when the surface is observed by SEM, that is, the 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 composite monolith ion exchanger and the inside of the skeleton is not preferable. 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 particles attached to the surface of the skeleton of the composite monolith ion exchanger in the water-wet state is the diameter or size of the particles obtained by observing the SEM image of the composite monolith ion exchanger in the dry state. Further, the value calculated by multiplying the swelling rate when the dry state is changed to the wet state, or the diameter or size of the particulates obtained by observing the SEM image of the composite monolith in the dry state before introducing the ion exchange group And a value calculated by multiplying the swelling ratio before and after introduction of the ion exchange group. Specifically, the diameter of the composite monolith ion exchanger in the water wet state is x4 (mm), the diameter of the composite monolith ion exchanger in the dry state obtained by drying the composite monolith ion exchanger in the water wet state. Is y4 (mm), and the diameter or size of the particles in the SEM image of the dried composite monolith ion exchanger observed by SEM is z4 (μm). The diameter or size (μm) of the particles of the monolith ion exchanger is expressed by the following formula: “diameter or size (μm) of the particles of the composite monolith ion exchanger in a water-wet state” = z4 × (x4 / y4) Is calculated. Then, the diameter or size of all particles observed in the SEM image of the composite monolith ion exchanger in the dry state is measured, and based on the value, all particles in one field of view SEM image, etc. The diameter or size of the water in a wet state is calculated. The SEM observation of the dried composite monolith ion exchanger is performed at least three times, and the diameter or size of the whole particle in the SEM image in the water-wet state is calculated in all fields of view. It is confirmed whether or not a particle body or the like at 4 to 40 μm is observed, and when it is confirmed in the entire visual field, the diameter or size is 4 to 40 μm in a wet state on the skeleton surface of the composite monolith ion exchanger. It is determined that the particle body at 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. is 40% or more in the wet state in all the particles in the entire visual field, the skeleton surface of the composite monolith ion exchanger is obtained. It is determined that the proportion of 4 to 40 μm particles in the wet state is 70% or more in all particles formed in the above. 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 composite monolith ion exchanger covered with all the particulates is 40% or more. In addition, the diameter or size of the particles of the composite monolith in the dry state before the introduction of the ion exchange group and the composite monolith ion exchange in the wet state with respect to the dry composite monolith when the ion exchange group is introduced into the monolith in the dry state If the swelling rate of the body is known, the diameter or size of the particles of the composite monolith in the dry state is multiplied by the swelling rate to obtain the diameter or size of the particles of the composite monolith ion exchanger in the water wet state. In the same manner as described above, the diameter or size of the particles of the composite monolith ion exchanger in the water wet state, the ratio of the particles of 4 to 40 μm in the water wet state, etc. in the total particles, etc. In addition, the coverage ratio of the surface of the skeleton layer with particle bodies can be obtained.

  When the coverage of the skeletal phase surface with particles and the like is less than 40%, the effect of improving the contact efficiency between the fluid and the inside of the skeleton of the composite monolith ion exchanger and the skeleton surface is reduced, and the uniformity of the ion exchange behavior is reduced. Since it will be damaged, it is not preferable. Examples of the method for measuring the coverage with the particulates include an image analysis method using a monolith (dry body) SEM image.

  The total pore volume of the composite monolith ion exchanger is the same as the total pore volume of the composite monolith. That is, even when the ion exchange group is introduced into the composite monolith to swell and increase the opening diameter, the total pore volume hardly changes because the skeletal phase is thick. If the total pore volume is less than 0.5 ml / g, the pressure loss during fluid permeation increases, which is not preferable. On the other hand, if the total pore volume exceeds 5 ml / g, the ion exchange capacity per volume is not preferable. Is unfavorable because it decreases. Note that the total pore volume of the composite monolith (monolith intermediate, composite monolith, composite monolith ion exchanger) is the same in both the dry state and the water state.

  Note that the pressure loss when water is permeated through the composite monolith ion exchanger is the same as the pressure loss when water is permeated through the composite monolith.

  The composite monolith ion exchanger of the present invention has an ion exchange capacity per volume in a water-wet state of 0.2 mg equivalent / ml or more, preferably 0.3 to 1.8 mg equivalent / ml. If the ion exchange capacity per volume is less than 0.2 mg equivalent / ml, the desalting efficiency is lowered, which is not preferable. In addition, the ion exchange capacity per weight in the dry state of the composite monolith ion exchanger of the present invention is not particularly limited, but since the ion exchange groups are uniformly introduced to the skeleton surface and the skeleton inside the composite monolith, 5 mg equivalent / g. The ion exchange capacity of the organic porous material in which the ion exchange group is introduced only on the surface of the skeleton cannot be determined depending on the kind of the organic porous material or the ion exchange group, but is 500 μg equivalent / g at most.

  Examples of the ion exchange group to be introduced into the composite monolith of the present invention include cation exchange groups such as a sulfonic acid group, a carboxylic acid group, an iminodiacetic acid group, a phosphoric acid group, and a phosphoric acid ester group; a quaternary ammonium group and a tertiary amino group. And anion exchange groups such as secondary amino group, primary amino group, polyethyleneimine group, tertiary sulfonium group, and phosphonium group.

  In the composite monolith ion exchanger of the present invention, the introduced ion exchange groups are uniformly distributed not only on the surface of the skeleton of the composite monolith but also inside the skeleton phase. Here, “the ion exchange groups are uniformly distributed” means that the distribution of the ion exchange groups is uniformly distributed at least on the order of μm on the surface of the skeleton phase and inside the skeleton phase. The distribution of ion exchange groups can be confirmed relatively easily by using EPMA or the like. In addition, when the ion exchange groups are uniformly distributed not only on the surface of the composite monolith but also inside the skeleton phase, the physical and chemical properties of the surface and the interior can be made uniform, so that the swelling and shrinkage can be prevented. Durability is improved.

  The composite monolith ion exchanger of the present invention has a thickness of 1 mm or more, and is distinguished from a membrane-like porous body. When the thickness is less than 1 mm, the ion exchange capacity per porous body is extremely reduced, which is not preferable. The thickness of the composite monolith ion exchanger is preferably 3 mm to 1000 mm. In addition, the composite monolith ion exchanger of the present invention has high mechanical strength because the basic structure of the skeleton is a continuous pore structure.

The composite monolith ion exchanger of the present invention is obtained by stirring a mixture of an oil-soluble monomer containing no ion exchange group, a first crosslinking agent having at least two or more vinyl groups in one molecule, a surfactant and water. Preparing a water-in-oil emulsion and then polymerizing the water-in-oil emulsion to obtain a monolithic organic porous intermediate having a continuous macropore structure with a total pore volume of 5 to 30 ml / g, vinyl monomer, A mixture comprising a second crosslinking agent having at least two vinyl groups in one molecule, an organic solvent that dissolves the vinyl monomer or the second crosslinking agent but does not dissolve the polymer formed by polymerization of the vinyl monomer, and a polymerization initiator. Step II for preparing the compound II. The mixture obtained in Step II is allowed to stand, and polymerization is performed in the presence of the monolithic organic porous intermediate obtained in Step I II When the monolithic organic porous material is produced by performing the IV step of introducing an ion exchange group into the monolithic organic porous material obtained in the steps I and III, the following (1) to (5):
(1) The polymerization temperature in step III is at least 5 ° C. lower than the 10-hour half-life temperature of the polymerization initiator;
(2) The mol% of the second cross-linking agent used in step II is at least twice the mol% of the first cross-linking 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; obtained by performing Step II or Step III under conditions that satisfy at least one of the conditions .

(Method for producing monolith intermediate)
In the method for producing a monolith according to the present invention, in the step I, an oil-soluble monomer not containing an ion exchange group, a first crosslinking agent having at least two or more vinyl groups in one molecule, a mixture of a surfactant and water are stirred. In this step, a water-in-oil emulsion is prepared, and then the water-in-oil emulsion is polymerized to obtain a monolith intermediate having a continuous macropore structure having a total pore volume of 5 to 30 ml / g. The step I for obtaining the monolith intermediate may be performed according to the method described in JP-A-2002-306976.

  Examples of the oil-soluble monomer that does not contain an ion exchange group include an oleophilic monomer that does not contain an ion exchange group such as a carboxylic acid group, a sulfonic acid group, and a quaternary ammonium group, 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 alone or in combination of two or more.

  Examples of the first crosslinking agent having at least two or more vinyl groups in one molecule include divinylbenzene, divinylnaphthalene, divinylbiphenyl, and ethylene glycol dimethacrylate. These crosslinking agents can be used singly or in combination of two or more. A preferred first cross-linking agent is an aromatic polyvinyl compound such as divinylbenzene, divinylnaphthalene, and divinylbiphenyl because of its high mechanical strength. The amount of the first crosslinking agent used is 0.3 to 10 mol%, particularly 0.3 to 5 mol%, and more preferably 0.3 to 3 mol%, based on the total amount of the vinyl monomer and the first crosslinking agent. Is preferred. If the amount of the first 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 monolith becomes more brittle and the flexibility is lost, and the amount of ion exchange groups introduced decreases, which is not preferable.

  The surfactant 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, and sorbitan monooleate, Nonionic surfactants such as sorbitan monolaurate, sorbitan monopalmitate, sorbitan monostearate, sorbitan trioleate, polyoxyethylene nonylphenyl ether, polyoxyethylene stearyl ether, polyoxyethylene sorbitan monooleate; potassium oleate Anionic surfactants such as sodium dodecylbenzenesulfonate and dioctyl sodium sulfosuccinate; cationic surfactants such as distearyldimethylammonium chloride; amphoteric surfactants such as lauryldimethylbetaine can be used . These surfactants can be used alone 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%.

  In Step I, a polymerization initiator may be used as necessary when forming a 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, 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.

  There is no particular limitation on the mixing method when mixing the oil-soluble monomer containing no ion exchange group, the first cross-linking agent, the surfactant, water and the polymerization initiator to form a water-in-oil emulsion, A method of mixing components all at once, an oil-soluble monomer, a first crosslinking agent, 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 For example, a method in which each component is mixed after being uniformly dissolved separately 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 obtained in Step I has a continuous macropore structure. When this coexists 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 as a template, or particles or the like are formed on the surface of the skeleton phase of the co-continuous structure. Or The monolith intermediate 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 porous body becomes brittle and the flexibility is lost, which is not preferable.

  The total pore volume of the monolith intermediate is 5-30 ml / g, preferably 6-28 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 tends to be non-uniform, and in some cases, the structure collapses, which is not preferable. In order to set the total pore volume of the monolith intermediate in the above numerical range, the ratio (weight) of the monomer to water may be set to approximately 1: 5 to 1:35.

  When the ratio of this monomer to water is approximately 1: 5 to 1:20, a monolith intermediate having a total pore volume of 5 to 16 ml / g and a continuous macropore structure can be obtained and obtained through Step III. The obtained composite monolithic organic porous body is the first organic porous body. Further, if the blending ratio is approximately 1:20 to 1:35, a monolith intermediate having a total pore volume of more than 16 ml / g and a continuous macropore structure of 30 ml / g or less can be obtained. The organic porous body of the composite monolith obtained through the above is obtained as the second organic porous body.

  Moreover, the average diameter of the opening (mesopore) which is an overlap part of a macropore and a macropore is 20-100 micrometers in a dry state in a monolith intermediate. When the average diameter of the openings is less than 20 μm, the opening diameter of the monolith obtained after polymerizing the vinyl monomer becomes small, and the pressure loss at the time of passing water becomes large, 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 it becomes difficult to form a water flow path uniformly. 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.

(Production method of composite monolith)
Step II is an organic solvent in which a vinyl monomer, a second cross-linking agent having at least two vinyl groups in one molecule, a vinyl monomer or a second cross-linking agent dissolves, but a polymer formed by polymerization of the vinyl monomer does not dissolve. And a step of preparing a mixture comprising 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 is not particularly limited as long as it is a lipophilic vinyl monomer that contains a polymerizable vinyl group in the molecule and has high solubility in an organic solvent. 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 suitably used in the present invention is an aromatic vinyl monomer such as styrene or vinyl benzyl chloride.

  The added amount of these vinyl monomers is 3 to 40 times, preferably 4 to 30 times, by weight with respect to the monolith intermediate coexisting during polymerization. If the amount of vinyl monomer added is less than 3 times that of the porous body, it is preferable because the particles cannot be formed in the skeleton of the produced monolith, and the ion exchange capacity per volume after introduction of the ion exchange groups is reduced. Absent. On the other hand, if the amount of vinyl monomer added exceeds 40 times, the opening diameter becomes small and the pressure loss during fluid permeation increases, which is not preferable.

  As the second crosslinking agent used in Step II, one having at least two polymerizable vinyl groups in the molecule and having high solubility in an organic solvent is preferably used. 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 is preferably 0.3 to 20 mol%, particularly 0.3 to 10 mol%, based on the total amount of the vinyl monomer and the second 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 monolith becomes more brittle and the flexibility is lost, and the amount of ion exchange groups introduced decreases, which is not preferable.

  The organic solvent used in step II is an organic solvent that dissolves the vinyl monomer and the second cross-linking agent but does not dissolve the polymer formed by polymerization of the vinyl monomer, in other words, a poor solvent for the polymer formed by polymerization of the vinyl monomer. It is. 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, a compound that generates radicals by heat and light irradiation is preferably used. The polymerization initiator is preferably oil-soluble. Specific examples of the polymerization initiator used in the present invention include 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, tetramethylthiuram disulfide and the like. The amount of 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 second crosslinking agent. .

  In step III, the mixture obtained in step II is allowed to stand, and in the presence of the monolith intermediate obtained in step I, polymerization is performed to obtain a composite monolith. The monolith intermediate used in the step III plays a very important role in creating the monolith having the novel structure of the present invention. As disclosed in JP-A-7-501140 and the like, when a vinyl monomer and a second cross-linking agent are allowed to stand in a specific organic solvent in the absence of a monolith intermediate, a particle aggregation type monolithic organic material is obtained. A porous body is obtained. On the other hand, when a monolith intermediate having a continuous macropore structure is present in the polymerization system as in the present invention, the structure of the monolith after polymerization changes dramatically, the particle aggregation structure disappears, and the specific skeleton described above is lost. A monolith having a 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 to exist in the reaction vessel. When the monolith intermediate is placed in the reaction vessel, there is a gap around the monolith in plan view. Or a monolith intermediate in the reaction vessel with no 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 crosslinking agent are adsorbed and distributed on the monolith intermediate, so the gaps in the reaction vessel A particle aggregate structure is not generated in the portion.

  In step III, the monolith intermediate is placed in a reaction vessel impregnated with the mixture (solution). As described above, the blending ratio of the mixture obtained in Step II and the monolith intermediate is 3 to 40 times by weight, preferably 4 to 30 times by weight, relative to the monolith intermediate. It is suitable to mix. Thereby, it is possible to obtain a monolith having a specific 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.

  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 heat polymerization, the vinyl monomer adsorbed and distributed on the skeleton of the monolith intermediate and the crosslinking agent are polymerized in the skeleton to form the specific skeleton structure. After completion of the polymerization, the content is taken out and extracted with a solvent such as acetone for the purpose of removing unreacted vinyl monomer and organic solvent to obtain a monolith having a specific skeleton structure.

  When the above-mentioned composite monolith is produced, the skeleton, which is the characteristic structure of the present invention, is obtained by performing the II step or the III step under the conditions satisfying at least one of the following conditions (1) to (5). A composite monolith having particles or the like formed on the surface 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 mol% of the second cross-linking agent used in step II is at least twice the mol% of the first cross-linking 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.

  The preferred 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.

(Description of (2))
When the mol% of the second cross-linking agent used in Step II is set to be twice or more of the mol% of the first cross-linking agent used in Step I, the composite monolith of the present invention 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 second crosslinker mol% used in step II is not particularly limited, but if the second crosslinker mol% is extremely large, cracks occur in the monolith after polymerization, and the brittleness of the monolith proceeds and flexibility is increased. This is not preferable because it causes a problem that the amount of ion exchange groups to be lost is reduced. A preferred multiple of the second crosslinking agent mol% is 2 to 10 times. On the other hand, even when the mol% of the first cross-linking agent used in step I is set to be twice or more the mol% of the second cross-linking agent used in step II, the formation of particles on the surface of the skeleton phase does not occur. The composite monolith of the present invention cannot be obtained.

(Explanation of (3))
When 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, the composite monolith of the present invention 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, a monomer having a structure different from that of the monomer used for forming the monolith intermediate used in Step I, that is, a monomer other than the monomer used for forming the monolith intermediate used in Step I is used in Step II to polymerize in Step III. The monomer used in Step II is uniformly distributed and impregnated into the monolith intermediate, but when the polymerization proceeds and the polymer is produced, the produced polymer is not compatible with the monolith intermediate. Separation proceeds, and the produced polymer is considered to be excluded in the vicinity of the surface of the skeleton phase of the monolith intermediate, and irregularities such as particles are formed on the surface of the skeleton phase.

(Explanation of (4))
When the organic solvent used in step II is a polyether having a molecular weight of 200 or more, the composite monolith of the present invention is obtained. 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 is not particularly limited as long as it is 200 or more. However, when the molecular weight is too high, the viscosity of the mixture prepared in the step II becomes high, and it is difficult to impregnate the monolith intermediate. Therefore, it is not preferable. 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.

(Explanation of (5))
When the concentration of the vinyl monomer used in Step II is 30% by weight or less in the mixture in Step II, the composite monolith of the present invention is obtained. 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.

  The composite monolith obtained in the step III includes an organic porous body composed of a continuous skeleton phase and a continuous pore phase, a large number of particles fixed to the skeleton surface of the organic porous body, or a skeleton surface of the organic porous body. It is a composite structure with a number of protrusions formed on it. The continuous skeleton phase and the continuous pore phase of the organic porous body can be observed by SEM images. The basic structure of the organic porous body is a continuous macropore structure or a co-continuous structure.

  The continuous macropore structure in the composite monolith is such that bubble-shaped macropores overlap each other, and the overlapping portion becomes an opening having an average diameter of 20 to 100 μm in a dry state. The bicontinuous structure in the composite monolith has an average thickness. Is composed of a three-dimensionally continuous skeleton of 0.8 to 40 μm in a dry state and three-dimensionally continuous pores having an average diameter of 8 to 80 μm by drying between the skeletons.

  Step IV is a step of introducing an ion exchange group into the composite monolith obtained in step III. According to this introduction method, the porous structure of the obtained composite monolith ion exchanger can be strictly controlled.

  The method for introducing an ion exchange group into the composite monolith is not particularly limited, and a known method such as polymer reaction or graft polymerization can be used. For example, as a method of introducing a sulfonic acid group, if the composite monolith is a styrene-divinylbenzene copolymer, etc., a method of sulfonation using chlorosulfuric acid, concentrated sulfuric acid, or fuming sulfuric acid; radical initiating groups uniformly on the composite monolith 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. In addition, as a method of introducing a quaternary ammonium group, if the composite monolith is a styrene-divinylbenzene copolymer or the like, a method of introducing a chloromethyl group with chloromethyl methyl ether or the like and then reacting with a tertiary amine; A method of producing monolith by copolymerization of chloromethylstyrene and divinylbenzene and reacting with a tertiary amine; uniformly introducing a radical initiating group or chain transfer group into the monolith on the skeleton surface and inside the skeleton, and N, N, N- Examples include a method of graft polymerization of 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 sulfonic acid group includes a method of introducing a sulfonic acid group into a styrene-divinylbenzene copolymer using chlorosulfuric acid, and a method of introducing a quaternary ammonium group includes styrene. -Introducing a chloromethyl group into the divinylbenzene copolymer with chloromethyl methyl ether, etc., then reacting with a tertiary amine, or producing a monolith by copolymerization of chloromethylstyrene and divinylbenzene and reacting with a tertiary amine The method is preferable in that the ion exchange group can be introduced uniformly and quantitatively. The 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 ester groups; quaternary ammonium groups, tertiary amino groups, and secondary amino groups. Groups, primary amino groups, polyethyleneimine groups, tertiary sulfonium groups, phosphonium groups and the like.

  In this invention, it does not restrict | limit especially as a granular ion exchange resin, The well-known ion exchange resin used for a water treatment is mentioned.

  Although it does not restrict | limit especially as a mixture of a monolith and an ion exchange resin, The layered body by which the monolith phase and the ion exchange resin phase were laminated | stacked in the water flow direction (direction in which discharge | emission ion migrates) is mentioned. The layered body of monolith and ion exchange resin is a monolithic sponge-like structure, so that it does not mix with the ion exchange resin and can be filled in phase without using partition means such as an ion exchange membrane in the container. . The volume ratio of the monolith phase and the ion exchange resin phase in the layered body is not particularly limited, and is appropriately determined depending on the type of ion exchange group, the purpose of treating the water to be treated, and the like. Further, the laminated structure of the layered body is not particularly limited, and the monolith phase and the ion exchange resin phase, the ion exchange resin phase and the monolith phase 2 in order from the ion exchange membrane on one side to the ion exchange membrane on the other side. Layer structure; monolith phase, ion exchange resin phase and monolith phase, three layer structure of ion exchange resin phase, monolith phase and ion exchange resin phase; four layer structure which is repetition of monolith phase and ion exchange resin phase. Among these, the configuration in which the monolith phase is arranged in the vicinity of the treated water inlet improves the removal rate of hardness components such as calcium ions in the decation chamber, and removes anions such as carbonic acid and silica in the deanion chamber. Is preferable in terms of improvement. In the deanion chamber, it is preferable to dispose the cation monolith in the vicinity of the treated water outlet from the viewpoint of reliably removing a trace amount of cations that could not be removed in the decation chamber.

The ionic form of the mixture of the monolith and the ion exchange resin is not particularly limited, but a salt form and a regenerated form mixture are preferred in that they can alleviate swelling and shrinkage associated with the ion exchange reaction. In the present invention, the swelling / shrinkage mitigating effect of the monolith / ion exchange resin mixture alone is not sufficient, and the physical expansion / contraction effect of the monolith is added to ensure adhesion in the deionization chamber. . The expansion and contraction of the mixture of monolith and ion exchange resin will be described by taking a cation cell as an example. The cation cell of FIG. 17A is composed of 40 ml of R—Na granular cation exchange resin (cross section 4 × 5 = 20 cm ² , length between electrodes 2 cm) in order from the cathode side to the anode side, RH granular cation exchange resin. 80 ml (cross section 4 × 5 = 20 cm ² , electrode length 4 cm) and R—Na cation monolith 40 ml (cross section 4 × 5 = 20 cm ² , electrode length 2 cm) are filled. When continuous water flow / continuous regeneration is performed for the cation cell, usually, the R—Na particulate cation exchange resin is partially regenerated and swells, and the RH particulate cation exchange resin does not change, and the R—Na cation monolith is not changed. Regenerates and swells. At this time, although the cation monolith regenerated from R-Na to R-H swells, it crushes into a sponge shape (concave shape) and absorbs the swelling of the R-Na granular cation exchange resin. The degree is improved and the container is well balanced (FIG. 17B). On the other hand, when the above-mentioned cation cell is subjected to continuous water flow / regeneration, the ion load of the water to be treated is high and the ion accumulation tendency is more balanced than the initial filling state. Side) to the treated water outlet (anode, regeneration side), and the continuous treatment is performed with the ion exchanger length extended. In this case, the R—Na particulate cation exchange resin does not change, the RH particulate cation exchange resin partially changes into a salt form and contracts, and the R—Na cation monolith is regenerated to RH and swells. At this time, the cation monolith regenerated from R—Na to R—H compensates for the volume reduction of the R—H granular cation exchange resin. (FIG. 17C). In this example, the R—Na granular cation exchange resin and the R—H granular cation exchange resin are described as being packed in layers, but the present invention is not limited to this, and may be used in a mixed manner. Has the effect of.

  In the present invention, the water to be treated is intended for deionization treatment and is not particularly limited as long as it does not contain turbidity. For example, industrial water or city water having a turbidity of about 1 degree or less. Can be mentioned.

  Next, the electric deionized water production apparatus according to the first embodiment of the present invention will be described with reference to FIG. FIG. 18 is a schematic view showing the structure of the electric deionized water production apparatus of this example. The electric deionized water production apparatus 20A of FIG. 18 includes an anion cell 20a that mainly removes anionic impurities from the water to be treated, and a cation cell 20b that mainly removes cationic impurities from the treated water of the anion cell 20a. It consists of

  The anion cell 20a includes an anion monolith 14 and an anion exchange resin 11 in order from the one anion exchange membrane 2 side into a deionization chamber partitioned by the one side anion exchange membrane 2 and the other side cation exchange membrane 1. To form a deanion chamber 7 and an anode 10 outside the anion exchange membrane 2 on one side and a cathode 9 outside the cation exchange membrane 1 on the other side. Supplied from the inlet 3a in the vicinity of the anion exchange membrane 2 on one side (anode side) in the deanion chamber 7, and in the vicinity of the cation exchange membrane 1 on the other side (cathode side) in the deanion chamber 7. The first treated water is obtained from the outlet 4a. That is, the water flow direction in the anion cell 20a of the anion cell 20a is from the left to the right, which is the solid arrow direction in FIG. The filling ratio of the anion monolith 14 and the anion exchange resin 11 can be arbitrarily determined depending on the properties of the water to be treated, but preferably the monolith: ion exchange resin is 1: 0.5 to 1:10 by volume. .

  On the other hand, the cation cell 20b includes a cation monolith 13 and a cation exchange resin in order from the cation exchange membrane 1 to the deionization chamber partitioned by the cation exchange membrane 1 on the one side and the cation exchange membrane 1 on the other side. 12, a decation chamber 6 is formed, a cathode 9 is arranged outside the cation exchange membrane 1 on one side, and an anode 10 is arranged outside the cation exchange membrane 1 on the other side, and an anion cell 20a. Of the treated water (first treated water) from the inlet 3b in the vicinity of the cation exchange membrane 1 on one side (cathode side) in the decation chamber 6 and the other side (anode) in the decation chamber 6 The treated water (second treated water) is obtained from the outlet 4b near the cation exchange membrane 1 on the side). That is, the water flow direction in the cation chamber 6 of the cation cell 20b is from the left to the right, which is the direction of the solid arrow in FIG. The filling ratio of the cation monolith 13 and the cation exchange resin 12 can be arbitrarily determined depending on the properties of the water to be treated, but preferably the monolith: ion exchange resin is 1: 0.5 to 1:10 by volume. .

  As the anionic monolith 14 filled in the deanion chamber 7 of the anion cell 20a of this example and the cation monolith 13 filled in the decation chamber 6 of the cation cell 20b, the above-mentioned monolithic organic porous ion exchanger is used. Is preferred. Moreover, as the shape of the decation ion chamber 6 and the deanion ion chamber 7, if an electric field can be applied so that the ions to be excluded migrate in the direction opposite to the water flow direction in the mixed ion exchanger, Although not particularly limited, for example, a cylindrical shape or a rectangular parallelepiped shape is preferable from the viewpoint of ease of manufacturing the constituent members. Moreover, the distance to which the water to be treated moves, that is, the effective thickness of the mixed ion exchanger packed layer constituting the decation ion chamber 6 and the deanion chamber 7 is 20 to 600 mm, preferably 30 to 300 mm. This is preferable in that the deionization process can be reliably performed while suppressing the electric resistance value and the water flow differential pressure.

  Examples of the cation exchange membrane, the anion exchange membrane, the cathode, the anode, the arrangement form of the electrode and the ion exchange membrane, the arrangement form of the direct current, the method of applying the direct current, etc. include those described in JP-A-2003-334560. . In the anion cell 20a, a non-conductive spacer 8 such as a polyolefin mesh is interposed between the anode and the anion exchange membrane in order to avoid direct contact between them. Thereby, it is possible to prevent the deterioration of the anion exchange membrane due to the strong oxidation action on the anode side.

  In the anion cell 20a and the cation cell 20b, the method for inflow of the water to be treated into the mixed ion exchanger and the method for collecting water from the mixed ion exchanger in the treated water are not particularly limited and are containers filled with the mixed ion exchanger. What is necessary is just to flow in treated water or flow out treated water from an inflow port or an outflow port installed in the vicinity of the ion exchange membrane. Also, for example, in order to form an even flow of water to be treated in the deionization chamber, the distribution pipes and water collection pipes having pores in the pipes are concentrically or equidistantly paralleled in line with the shape of the deionization chamber. Using a method of embedding in an ion exchanger, a method of cutting a groove in the monolith treated water collection section or the first treated water introduction / distribution section, and providing the monolith itself with a treated water collection function or a treated water distribution function Also good.

  In the electric deionized water production apparatus 20A of FIG. 18, the ion exchanger filled in the anion cell 20a and the cation cell 20b is not limited to the above, and for example, the anion monolith 14 and the anion exchange resin are added to the anion cell 20a. 11 is not particularly limited, the ion exchanger filled in the cation cell 20b is not particularly limited. For example, a known cation monolith single bed, a cation exchange resin single bed, or a mixture of a known cation monolith and a cation exchange resin, A cation monolith single bed comprising a composite monolith ion exchanger used in the invention can be used. Further, for example, when the cation cell 20b is filled with the cation monolith 13 and the cation exchange resin 12, the ion exchanger filled in the anion cell 20a is not particularly limited. For example, a known anion monolith single bed, anion exchange resin single bed Alternatively, a known mixture of an anionic monolith and an anion exchange resin, an anionic monolith single bed comprising a composite monolith ion exchanger used in the present invention, and the like can be used.

  In addition, the operation method of the electric deionized water production apparatus 20A of this example may be either continuous operation or intermittent operation. For example, the continuous operation method by continuous water flow and continuous energization of the water to be treated and the treatment target. Examples include an intermittent operation method in which water flow is stopped for a certain period of time and direct current is supplied only during the water stoppage time.

In the anion cell 20a, water to be treated is introduced from an inlet 3a in the vicinity of the anion exchange membrane 2 on the anode 10 side of the deanion chamber 7. Next, the water to be treated moves to the cathode 9 side while adsorbing and removing the anions Y ⁻ in the anion monolith 14 and the anion exchange resin 11, and serves as the first treated water in the cathode 9 side cation exchange membrane of the deanion chamber 7. 1 is discharged from the outlet 4a in the vicinity. Next, the first treated water is introduced into the vicinity of the cathode 9 side cation exchange membrane 1 in the decation chamber 6 of the cation cell 20b through the communication pipe 5a and the inlet 3b. Next, the first treated water, which is the treated water, moves to the anode 10 side while adsorbing and removing the cation X ⁺ in the cation monolith 13 and the cation exchange resin 12, and serves as the second treated water in the anode of the decation chamber 6. It is discharged from the 10-side cation exchange membrane 1 vicinity outlet 4b.

The anion Y ⁻ adsorbed on the anion monolith 14 and the anion exchange resin 11 in the deanion chamber 7 is electrically generated by a direct current applied between the cathode 9 and the anode 10 disposed at both ends of the deanion chamber 7. The anion Y ⁻ passes through the anion exchange membrane 2 on the anode 10 side and is discharged to the anode chamber (not shown). Similarly, the cation X ⁺ adsorbed by the cation monolith 13 and the cation exchange resin 12 in the decation chamber 6 is applied to the direct current applied between the cathode 9 and the anode 10 disposed at both ends of the decation chamber 6. Electrophoresis is caused by electric current, passes through the cation exchange membrane 1 on the cathode 9 side, and is discharged to the cathode chamber (not shown).

  The impurity anions discharged into the anode chamber flow in from the anode chamber inlet, are taken into the electrode water flowing out from the anode chamber outlet, and are discharged out of the system. Similarly, impurity cations discharged to the cathode chamber flow into the electrode chamber from the cathode chamber inlet, and are taken into the electrode water flowing out from the cathode chamber outlet and discharged out of the system. The electrode water may be made to flow partially in the four electrode chambers by branching off a part of the water to be treated, or may be allowed to flow in two systems of an anodic water system and a cathodic water system, respectively. Moreover, electrode water may be always flowed and may be appropriately flowed intermittently.

  In this method, in the anion cell 20a, an anionic monolith phase is arranged in the vicinity of the inlet of the water to be treated, so that the removal rate of anions such as carbonic acid and silica is improved. This is particularly effective when containing a large amount of carbonic acid. According to this apparatus, since the monolith and the ion exchange resin are mixed in layers in the cell, it is possible to compensate for a decrease in the ion exchange capacity due to the use of the monolith. Further, the volume change due to the swelling and shrinkage reaction of the monolith and the ion exchange resin can be mitigated by the physical stretchability of the monolith, and the filling state in the deion exchange chamber can be kept uniform. In addition, since the impurity cation and the impurity anion are separately discharged outside the apparatus, they are not mixed in the apparatus unlike conventional electric deionized water production apparatuses, and calcium or Even when a hardness component such as magnesium is contained, no scale is generated in the apparatus.

  In addition to the above, for example, a method of treating the water to be treated with the cation cell 20b and then treating the treated water of the cation cell 20b with the anion cell 20a as the water passing method of the electric deionized water production apparatus 20A. Can do. According to this method, since water is first passed through the cation cell and calcium ions and magnesium ions are excluded, scale generation in the anion cell 20a can be prevented. Further, in the cation cell 20b, a cation monolith is provided in the vicinity of the water inlet to be treated. Since the phases are arranged, the exclusion rate of calcium ions and magnesium ions is improved. For this reason, this method is effective when processing the to-be-processed water containing hardness components, such as calcium and magnesium.

  In the electric deionized water production apparatus 20A of the present example, the mixed ion exchanger filled in the deanion chamber 7 is different from the above-described form in that the other side of the anion exchange membrane 2 from the one side (anode side). Examples include a form in which the anion exchange resin and the cation monolith are filled in order toward the cation exchange membrane 1, a form in which the anion monolith, the anion exchange resin, and the cation monolith are filled. The ion exchange membrane on the cathode side is determined as a cation exchange membrane or an anion exchange membrane depending on the ion exchanger filled in the vicinity. When the anion exchange resin and the cation monolith are filled, they can be buffered by the physical stretchability of the cation monolith, the filling state in the deanion chamber can be kept uniform, and a simple polishing function can be provided. In addition, when an anion monolith, an anion exchange resin, and a cation monolith are filled in this order, the removal rate of impurity anions such as carbonic acid and silica can be increased, and a simple polishing function is provided. The filling state in the deanion chamber can be kept uniform by physical stretchability. Moreover, an ion exchanger can be appropriately selected similarly for the mixed ion exchanger filled in the decation ion chamber 6. Similarly, for these forms, a method of treating the treated water with the cation cell 20b and then treating the treated water of the cation cell 20b with the anion cell 20a can be employed.

  Next, an electric deionized water production apparatus according to a second embodiment of the present invention will be described with reference to FIG. FIG. 19 is a schematic view showing the structure of the electric deionized water production apparatus of this example. In FIG. 19, the same components as those in FIG. 18 are denoted by the same reference numerals, description thereof is omitted, and different points are mainly described. The electric deionized water production apparatus 20B of FIG. 19 differs from FIG. 18 in that one set of electrodes is omitted and a decation ion chamber and a deanion ion chamber are provided between the pair of electrodes. That is, the electric deionized water production apparatus 20B of the present example is provided with the intermediate cation exchange membrane 1 between the cation exchange membrane 1 on one side and the anion exchange membrane 2 on the other side, and cation exchange on one side. The first deionization chamber partitioned by the membrane 1 and the intermediate cation exchange membrane 1 is filled with the cation monolith 13 and the cation exchange resin 12 in the order of water flow to form the decation chamber 6, and the other side anion exchange The second deionization chamber partitioned by the membrane 2 and the intermediate cation exchange membrane 1 is filled with the anion exchange resin 11 and the anion monolith 14 from the intermediate cation exchange membrane 1 side to form the deanion ion chamber 7, and one side The cathode 9 is arranged outside the cation exchange membrane 1 and the anode 10 is arranged outside the anion exchange membrane 2 on the other side, so that the water to be treated is anodized on the other side (anode side) in the deionization chamber 7. Supplying from the inlet 3a in the vicinity of the ion exchange membrane 2, the deionization chamber 7 The first treated water is obtained from the outlet 4a in the vicinity of the intermediate cation exchange membrane 1, and the first treated water is taken into the inlet in the vicinity of the cation exchange membrane 1 on one side (cathode side) in the decation chamber 6. The second treated water is obtained from the outlet 4b that is supplied from 3b and is in the vicinity of the intermediate cation exchange membrane 1 in the decation chamber 6.

  In the electric deionized water production apparatus 20B of FIG. 19, the ion exchanger filled in the deanion chamber 7 and the decation chamber 6 is not limited to the above, and for example, an anion monolith is provided in the deanion chamber 7. 14 and anion exchange resin 11 are filled, the ion exchanger filled in the decation chamber 6 is not particularly limited. For example, a known cation monolith single bed, a cation exchange resin single bed, or a known cation monolith and cation A mixture of exchange resins, a single monolithic cation monolith composed of a composite monolith ion exchanger used in the present invention, and the like can be used. For example, when the cation monolith 13 and the cation exchange resin 12 are filled in the decation chamber 6, the ion exchanger filled in the deanion chamber 7 is not particularly limited. For example, a known anion monolith single bed, anion An exchange resin single bed, a mixture of a known anion monolith and an anion exchange resin, an anion monolith single bed comprising a composite monolith ion exchanger used in the present invention, and the like can be used.

In electrodeionization water producing apparatus 20B, the for-treatment water which has flowed from the 10 side anion-exchange membrane 2 near the anode of Datsukage ion chamber 7 anion Y in the anion monolith 14 and anion exchange resin 11 ^- is adsorbed removed However, it moves to the intermediate cation exchange membrane 1 side and is discharged as first treated water from the intermediate cation exchange membrane 1 vicinity outlet 4b of the deanion ion chamber 7. Next, the first treated water is introduced into the decation chamber 6 from the vicinity of the cathode 9 side cation exchange membrane 1 in the decation chamber 6 through the communication pipe 5b. Next, the first treated water moves to the intermediate cation exchange membrane 1 side while adsorbing and removing the cation X ⁺ in the cation monolith 13 and the cation exchange resin 12, and serves as the second treated water in the middle of the decation chamber 6. It is discharged from the vicinity of the cation exchange membrane 1.

On the other hand, the cation X ⁺ adsorbed by the mixed cation exchanger in the decation chamber 6 is electrophoresed by a direct current applied between the cathode 9 and the anode 10 disposed at both ends of the apparatus 20B. Then, it passes through the cation exchange membrane 1 on the cathode 9 side and is discharged to the cathode chamber (not shown). Similarly, the anion Y ⁻ adsorbed on the mixed anion exchanger in the deanion chamber 7 is also electrophoresed by a direct current applied between the cathode 9 and the anode 10, and the anion on the anode 10 side. It passes through the ion exchange membrane 2 and is discharged to an anode chamber (not shown). That is, the direction of water flow in the deanion chamber 7 is from the right to the left, which is the direction of the solid line in FIG. In addition, the water flow direction in the decation ion chamber 6 is from the left to the right, which is the direction of the solid line, and the excluded cations migrate in the opposite direction to the water flow direction in the mixed ion exchanger. . The filling ratio of the monolith and the ion exchange resin in the decation chamber 6 and the deanion chamber 7 can be arbitrarily determined depending on the properties of the water to be treated, but preferably the monolith: ion exchange resin is in a volume ratio. 1: 0.5-1: 10. According to the electric deionized water production apparatus 20B of the second embodiment, the same effect as the electric deionized water production apparatus 20A of the first embodiment is obtained, and one set of electrodes is omitted. Thus, the device can be reduced in size and simplified.

  In addition to the above, as a water passing method of the electrical deionized water production apparatus 20B, for example, the water to be treated is treated in the decation chamber 6, and then the treated water in the decation chamber 6 is treated in the deanion chamber 7. Can be taken. According to this method, water is first passed through the decation ion chamber 6 to eliminate calcium ions and magnesium ions, so that scale generation in the deanion ion chamber 7 can be prevented. Since the cationic monolith phase is arranged in the vicinity, the exclusion rate of calcium ions and magnesium ions is improved. For this reason, it is effective when processing the to-be-processed water containing hardness components, such as calcium and magnesium.

  In the electric deionized water production apparatus 20B of the present example, the mixed ion exchanger filled in the decation chamber 6 can be exchanged from the cation exchange membrane 1 on one side (cathode side) in addition to the above form. Examples include a form in which the cation exchange resin and the anion monolith are filled in order toward the membrane 1, a form in which the cation monolith, the cation exchange resin, and the anion monolith are filled. The intermediate ion exchange membrane 1 is determined as a cation exchange membrane or an anion exchange membrane by an ion exchanger filled in the vicinity. When filled with a cation exchange resin and an anionic monolith, it can be buffered by the physical stretchability of the anionic monolith, the filling state in the decation chamber 6 can be kept uniform, and a simple polishing function can be provided. . In addition, when filled in the order of cation monolith, cation exchange resin, anion monolith, the removal rate of impurity cations including the above-mentioned hardness components such as calcium and magnesium can be increased, and a polishing function is provided. Can maintain a uniform filling state in the decation chamber 6 due to the physical stretchability of both monoliths. For the mixed ion exchanger filled in the deanion chamber 7, an ion exchanger can be selected as appropriate. Similarly, for these forms, a method of treating the water to be treated in the decation chamber 6 and then treating the treated water in the decation chamber 6 in the deanion chamber 7 can be adopted.

  Next, an electric deionized water production apparatus according to a third embodiment of the present invention will be described with reference to FIG. FIG. 20 is a schematic view showing the structure of the electric deionized water production apparatus of this example. 20, the same components as those in FIG. 19 are denoted by the same reference numerals, description thereof is omitted, and different points are mainly described. 20 is different from FIG. 19 in that the intermediate cation exchange membrane 1 and the cation exchange resin are both omitted. That is, the electric deionized water production apparatus 20C of this example is configured by arranging the anode 10 on the outside of the anion exchange membrane 2 on one side and the cathode 9 on the outside of the cation exchange membrane 1 on the other side. The anion monolith 14, the anion exchange resin 11, and the cation in this order from the anion exchange membrane 2 side on the one side (anode side) to the deionization chamber 15 partitioned by the anion exchange membrane 2 and the other cation exchange membrane 1. A monolith 13 is filled to form a deionization chamber 15, and water to be treated is supplied from an inlet 3 c near the anion exchange membrane 2 on one side in the deionization chamber 15, and the other side in the deionization chamber 15 is supplied. The treated water is obtained from the outlet 4c near the cation exchange membrane 1. That is, the water flow direction in the deionization chamber 15 is from the left to the right, which is the solid arrow direction in FIG.

In the electrical deionized water production apparatus 20 </ b> C, the water to be treated is introduced from the inlet 3 c in the vicinity of the anode 10 side anion exchange membrane 2 in the deionization chamber 15. Then, the water to be treated anion Y in the anion monolith 14 and anion exchange resin 11 ^- moved to while being adsorbed removed cathode 9 side, further the cathode 9 side while being adsorbed and removed cations X ⁺ in the cation monolith 13 And is discharged as treated water from an outlet 4c near the cathode 9 side cation exchange membrane 1 in the deionization chamber 15. According to the electric deionized water production apparatus 20C, the same effect as that of the electric deionized water production apparatus 20B can be obtained, and the intermediate cation membrane can be omitted to reduce the size and simplify the apparatus. In the case of the electric deionized water production apparatus 20C, the migration direction of the anion Y ⁻ is opposite to the water flow direction, and the migration direction of the cation X ⁺ is the same direction as the water flow direction.

In the electric deionized water production apparatus 20C, the mixed ion exchanger filled in the deionization chamber 15 is changed from the anion exchange membrane 2 on one side to the cation exchange membrane 1 on the other side in addition to the above-described form. The form which fills the anion exchange resin 11 and the cation monolith 13 in order toward this is mentioned. Similarly, the inflow location of the water to be treated is not limited to the above embodiment, and the water to be treated is allowed to flow into the inlet near the cation exchange membrane 1 on the other side for the cation exchange. The cation X ⁺ is moved to the anode 10 side while adsorbing and removing the cation X ⁺ in the body, and further moved to the anode 10 side while adsorbing and removing the anion Y ⁻ in the anion exchanger, and processed from the outlet near the anion exchange membrane 2. It may be a method of obtaining water. The filling ratio of the monolith and the ion exchange resin in the deionization chamber 15 can be arbitrarily determined depending on the properties of the water to be treated, but preferably the monolith: ion exchange resin is 1: 0.5 to 1: 10.

  The electric deionized water production apparatus of the present invention can be applied and combined in the same way as a conventional ion exchange apparatus. For example, it can be a softening apparatus using only a decation chamber or a mixed bed type ion exchange in the latter stage. By attaching a vessel, the quality of the treated water can be further increased.

  EXAMPLES Next, although an Example is given and this invention is demonstrated more concretely, this is only an illustration and does not restrict | limit this invention.

Reference example 1
(Step I; production of monolith intermediate)
9.28 g of styrene, 0.19 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 having a continuous macropore structure. The average diameter of the openings (mesopores) where the macropores and macropores of the monolith intermediate were measured by mercury porosimetry was 40 μm, and the total pore volume was 15.8 ml / g.

(Manufacture of composite monolith)
Next, 36.0 g of styrene, 4.0 g of divinylbenzene, 60 g of 1-decanol, 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 is 6.6 mol% with respect to the total amount of styrene and divinylbenzene used in Step II, while the crosslink density of the monolith intermediate is 1.3 mol%, and the crosslink density ratio is 5.1 times. Met. Next, the monolith intermediate was cut into a disk shape having an outer diameter of 70 mm and a thickness of about 20 mm, and 3.2 g was collected. The separated monolith intermediate is placed in a reaction vessel having an inner diameter of 73 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 (step III).

  The results of observing the internal structure of the composite monolith (dried body) composed of the styrene / divinylbenzene copolymer thus obtained by SEM are shown in FIGS. The SEM images in FIGS. 1 to 3 are different in magnification, and are images at arbitrary positions on a cut surface obtained by cutting a monolith at an arbitrary position. As apparent from FIGS. 1 to 3, the composite monolith has a continuous macropore structure, and the surface of the skeletal phase constituting the continuous macropore structure is coated with particles having an average particle diameter of 4 μm. The particle coverage of the skeleton surface by the body and the like was 80%. 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 of the opening of the composite monolith measured by mercury porosimetry was 16 μm, and the total pore volume was 2.3 ml / g. The results are summarized in Tables 1 and 2. In Table 1, the preparation column shows the vinyl monomer, the crosslinking agent, the organic solvent used in Step II, and the monolith intermediate obtained in Step I in order from the left. Further, the particle bodies and the like are shown as particles.

(Production of complex monolith cation exchanger)
The composite monolith 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. The weight of the monolith was 19.6 g. To this, 1500 ml of dichloromethane was added and heated at 35 ° C. for 1 hour, then cooled to 10 ° C. or less, 98.9 g of chlorosulfuric acid was gradually added, and the temperature was raised and reacted at 35 ° C. for 24 hours. Thereafter, methanol was added to quench the remaining chlorosulfuric acid, which was then washed with methanol to remove dichloromethane and further washed with pure water to obtain a composite monolith cation exchanger.

  The swelling rate before and after the reaction of the obtained cation exchanger was 1.3 times, and the ion exchange capacity per volume was 1.11 mg equivalent / ml in a water wet state. The average diameter of the openings of the organic porous ion exchanger in the water wet state was 21 μm as estimated from the value of the organic porous body and the swelling ratio of the cation exchanger in the water wet state. The average particle size of the particles was 5 μm. The particle coverage of the skeletal surface with all particles was 80%, and the total pore volume was 2.3 ml / g. Moreover, the ratio for which the particle body of 4-7 micrometers of particle | grains accounts to the whole particle body was 90%. The differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.057 MPa / m · LV, which is a lower pressure loss than that required for practical use. It was. Further, the length of the ion exchange zone was 9 mm, showing a remarkably short value. The results are summarized in Table 2.

  Next, in order to confirm the distribution state of the sulfonic acid group in the composite monolith cation exchanger, the distribution state of sulfur atoms was observed by EPMA. The results are shown in FIGS. 4 and 5, the left and right photographs correspond to each other. FIG. 4 shows the distribution of sulfur atoms on the surface of the cation exchanger, and FIG. 5 shows the distribution of sulfur atoms in the cross-section (thickness) direction of the cation exchanger. 4 and 5, it can be seen that the sulfonic acid groups are uniformly introduced on the skeleton surface of the cation exchanger and inside the skeleton (cross-sectional direction).

Reference Examples 2-5
(Manufacture of composite monolith)
The amount of vinyl monomer used, the amount of crosslinking agent used, the type and amount of organic solvent used, the porous structure of the monolith intermediate that coexists during polymerization in step III, the crosslinking density and the amount used, and the polymerization temperature are shown in Table 1. A monolith was produced in the same manner as in Reference Example 1 except for the change. The results are shown in Tables 1 and 2. Moreover, the result of having observed the internal structure of composite monolith (dry body) by SEM is shown in FIGS. 6 to 8 are of Reference Example 2, FIGS. 9 and 10 are of Reference Example 3, FIG. 11 is of Reference Example 4, and FIGS. 12 and 13 are of Reference Example 5. For Reference Example 2, the crosslinking density ratio (2.5 times), for Reference Example 3, the type of organic solvent (PEG; molecular weight 400), for Reference Example 4, the vinyl monomer concentration (28.0%), Reference Example For No. 5, the polymerization temperature (40 ° C .; 11 ° C. lower than the 10-hour half-life temperature of the polymerization initiator) was produced under conditions satisfying the production conditions of the present invention. From FIG. 6 to FIG. 13, what adhered to the skeleton surface of the composite monoliths of Reference Examples 3 to 5 were protrusions rather than particles. The “particle average diameter” of the protrusion is the average diameter of the protrusions (maximum diameter). From FIG. 6 to FIG. 13 and Table 2, the average diameter of the particles adhering to the surface of the monolith skeleton of Reference Examples 2 to 6 is 3 to 8 μm, and the particle coverage of the skeleton surface by all particles is 50 to 95%. there were. In addition, the proportion of Reference Example 2 in which particles having a particle diameter of 3 to 6 μm occupy the entire particle body is 80%, and the ratio of Reference Example 3 in which protrusions having a particle diameter of 3 to 10 μm occupy the entire particle is 80%. In Reference Example 4, the proportion of particles having a particle diameter of 3 to 5 μm in the total particle body was 90%, and in Reference Example 5, the proportion of particles having a particle diameter of 3 to 7 μm in the entire particle body was 90%. .

(Production of complex monolith cation exchanger)
The composite monolith produced by the above method was reacted with chlorosulfuric acid in the same manner as in Reference Example 1 to produce a composite monolith cation exchanger. The results are shown in Table 2. The average diameter of the continuous pores of the composite monolith cation exchanger in Reference Examples 2 to 5 is 21 to 52 μm, the average diameter of the particles attached to the skeleton surface is 5 to 13 μm, the skeleton surface due to all the particles, etc. The particle coverage was as high as 50 to 95%, the differential pressure coefficient was as small as 0.010 to 0.057 MPa / m · LV, and the ion exchange zone length was as extremely small as 8 to 12 mm. Moreover, the ratio for which the particle body with a particle size of 5-10 micrometers occupied to the whole particle body was 90%.

Reference Example 6
(Manufacture of composite monolith)
Table 1 shows the type and amount of vinyl monomer used, amount of crosslinking agent used, type and amount of organic solvent, monolith intermediate porous structure coexisting during polymerization in step III, crosslinking density and amount used. A monolith was produced in the same manner as in Reference Example 1 except for the change. The results are shown in Tables 1 and 2. Moreover, the result of having observed the internal structure of composite monolith (dry body) by SEM is shown in FIGS. What adhered to the skeleton surface of the composite monolith of Reference Example 6 was a protrusion. In the monolith of Reference Example 6, the average diameter of the maximum diameter of the protrusions formed on the surface was 10 μm, and the particle coverage of the skeletal surface with all the particulates 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%.

(Production of complex monolith anion exchanger)
The composite monolith 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. The weight of the composite monolith 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 resultant was washed with methanol to remove tetrahydrofuran, and further washed with pure water to obtain a monolith anion exchanger.

  The obtained composite anion exchanger had a swelling ratio of 2.0 times before and after the reaction, and the ion exchange capacity per volume was 0.32 mg equivalent / ml in a water-wet state. The average diameter of the continuous pores of the organic porous ion exchanger in the water wet state was 58 μm as estimated from the value of the monolith and the swelling ratio of the monolith anion exchanger in the water wet state. The average diameter of the body was 20 μm, the particle coverage of the skeletal surface with all particles was 100%, and the total pore volume was 2.1 ml / g. The ion exchange zone length was as short as 16 mm. 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%. The results are summarized in Table 2.

  Next, in order to confirm the distribution state of the quaternary ammonium groups in the porous anion exchanger, the anion exchanger was treated with an aqueous hydrochloric acid solution to form a chloride form, and then the distribution state of chlorine atoms was observed by EPMA. As a result, it was confirmed that the chlorine atoms were uniformly distributed not only on the skeleton surface of the anion exchanger but also inside the skeleton, and the quaternary ammonium groups were uniformly introduced into the anion exchanger.

Reference Example 7
(Manufacture of monolith intermediates)
A monolith intermediate was obtained in the same manner as in Reference Example 1.

(Manufacture of composite monolith)
38.0 g of styrene, 2.0 g of divinylbenzene, 60 g of 1-decanol, 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 is 3.3 mol% with respect to the total amount of styrene and divinylbenzene used in Step II, with a crosslink density ratio of 2.5 times the crosslink density of the monolith intermediate of 1.3 mol%. Met. Next, the monolith intermediate was cut into a disk shape having a diameter of 70 mm and a thickness of about 30 mm to obtain 3.3 g. The separated monolith intermediate is put in a reaction vessel having an inner diameter of 73 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 (step III).

  The internal structure of the monolith (dry body) containing 3.3 mol% of the crosslinking component composed of the styrene / divinylbenzene copolymer thus obtained was observed by SEM. The monolith 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 5 μm, and the particle coverage of the skeleton surface by all particles is 50%. Met. Moreover, the ratio for which the particle body with a particle size of 3-7 micrometers occupied to the whole particle body was 90%. Moreover, the average diameter of the opening of the monolith measured by mercury porosimetry was 35 μm, and the total pore volume was 3.8 ml / g.

(Production of complex monolith anion exchanger)
The monolith 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, then washed with pure water and isolated.

  The swelling ratio of the obtained monolith anion exchanger before and after the reaction was 1.5 times, and the anion exchange capacity per volume was 0.72 mg equivalent / ml in a water-wet state. The average diameter of the openings of the monolith anion exchanger in the water wet state was estimated to be 53 μm from the value of the monolith and the swelling ratio of the monolith anion exchanger in the water wet state, and the average particle diameter of the coated particles determined by the same method The diameter was 8 μm. In addition, the particle | grain coverage of the frame | skeleton surface by all the particle bodies etc. was 50%, and the total pore volume was 3.8 ml / g. Moreover, the ratio for which the particle diameter of 4-8 micrometers was occupied to the whole particle body was 90%.

  The differential pressure coefficient, which is an index of pressure loss when water is permeated, is 0.017 MPa / m · LV, which is a low pressure loss that does not cause any practical problems. Furthermore, when the ion exchange zone length regarding the fluoride ion of the monolith anion exchanger was measured, the ion exchange zone length at LV = 20 m / h was 14 mm, and amberlite which is a commercially available strong basic anion exchange resin. It was overwhelmingly shorter than the value (165 mm) of IRA402BL (made by Rohm and Haas).

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

Reference Example 8
(Manufacture of monoliths)
Except for changing the usage amount of the vinyl monomer, the usage amount of the crosslinking agent, the type and usage amount of the organic solvent, and the usage amount of the monolith intermediate coexisting during the polymerization in Step III to the blending amounts shown in Table 1, Example 1 and A monolith was produced in a similar manner. The results are shown in Tables 1 and 2. From the SEM photograph (not shown), the formation of particles and protrusions was not observed at all on the skeleton surface. From Table 1 and Table 2, when a monolith is produced under conditions deviating from the specific production conditions of the present invention, that is, conditions deviating from the requirements (1) to (5) above, particle formation on the surface of the monolith skeleton is caused. It turns out that it is not recognized.

(Production of monolith cation exchanger)
The monolith produced by the above method was reacted with chlorosulfuric acid in the same manner as in Reference Example 1 to produce a monolith cation exchanger. The results are shown in Table 2. The obtained monolith cation exchanger had an ion exchange zone length of 26 mm, which was a large value as compared with Reference Examples 1-7.

Reference Examples 9-11
(Manufacture of monoliths)
The amount of vinyl monomer used, the amount of crosslinking agent used, the type and amount of organic solvent used, the porous structure of the monolith intermediate that coexists during polymerization in step III, the crosslinking density, and the amount used were changed to the amounts shown in Table 1. Produced a monolith in the same manner as in Reference Example 1. The results are shown in Tables 1 and 2. For Reference Example 9, the crosslinking density ratio (0.2 times), for Reference Example 10, the type of organic solvent (2- (2-methoxyethoxy) ethanol; molecular weight 120), and for Reference Example 11, the polymerization temperature (50 C .: 1 ° C. lower than the 10-hour half-life temperature of the polymerization initiator) was produced under conditions that did not satisfy the production conditions of the present invention. The results are shown in Table 2. For the monoliths of Reference Examples 9 and 11, there was no particle formation on the skeleton surface. In Reference Example 10, the isolated product was transparent, and the porous structure was collapsed and disappeared.

(Production of monolith cation exchanger)
Except for Reference Example 10, the organic porous material produced by the above method was reacted with chlorosulfuric acid in the same manner as in Reference Example 8 to produce a monolith cation exchanger. The results are shown in Table 2. The obtained monolith cation exchanger had an ion exchange zone length of 23 to 26 mm, which was a large value as compared with Reference Examples 1 to 7.

Reference Example 12
(Manufacture of monoliths)
Reference Example 8 except that the use amount of the vinyl monomer, the use amount of the crosslinking agent, the use amount of the organic solvent, the porous structure and the use amount of the monolith intermediate coexisting during the polymerization in Step III were changed to the blending amounts shown in Table 1. A monolith was produced in the same manner as described above. The results are shown in Tables 1 and 2, and it can be seen that when a monolith is produced outside the specific production conditions of the present invention, no particle formation is observed on the surface of the monolith skeleton.

(Production of monolith anion exchanger)
The monolith 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, then washed with pure water and isolated. The results are shown in Table 2. The obtained monolith anion exchanger had an ion exchange zone length of 47 mm, which was a large value compared to Reference Examples 1-7. In Tables 1 and 2, the mesopore diameter and pore value are average values.

Reference Example 13
(Production of porous cation exchanger (known))
27.7 g of styrene, 6.9 g of divinylbenzene, 0.14 g of azobisisobutyronitrile and 3.8 g of sorbitan monooleate were mixed and dissolved uniformly. Next, the styrene / divinylbenzene / azobisisobutyronitrile / sorbitan monooleate mixture is added to 450 ml of pure water, stirred at 20,000 rpm for 2 minutes using a homogenizer, and a water-in-oil emulsion. Got. After emulsification, the water-in-oil emulsion was transferred to a stainless steel autoclave, sufficiently substituted with nitrogen, sealed, and allowed to polymerize at 60 ° C. for 24 hours. After completion of the polymerization, the content was taken out, extracted with Soxhlet for 18 hours with isopropanol, unreacted monomer and sorbitan monooleate were removed, and dried under reduced pressure at 40 ° C. overnight. 5 g of a porous material containing 14 mol% of a crosslinking component composed of a styrene / divinylbenzene copolymer obtained in this manner was collected, 500 g of tetrachloroethane was added, and the mixture was heated at 60 ° C. for 30 minutes, and then to room temperature. After cooling, 25 g of chlorosulfuric acid was gradually added and reacted at room temperature for 24 hours. Thereafter, acetic acid was added, the reaction product was poured into a large amount of water, washed with water and dried to obtain a porous cation exchanger. The ion exchange capacity of this porous material is 4.0 mg equivalent / g in terms of dry porous material, and sulfonic acid groups are uniformly introduced into the porous material by mapping of sulfur atoms using EPMA. It was confirmed. Further, as a result of SEM observation (not shown), the internal structure of the porous body has an open cell structure, and most of the macropores having an average diameter of 30 μm are overlapped, and the mesopores formed by the overlap of the macropores and the macropores. The average diameter was 5 μm and the total pore volume was 10.1 ml / g. The porous body was cut out to a thickness of 10 mm, and the water permeation rate was measured. As a result, it was 14,000 l / min · m ² · MPa.

Reference Example 14
(Production of porous anion exchanger (known))
A water-in-oil emulsion similar to that of Example 1 except that 18.0 g of p-chloromethylstyrene was used instead of 27.7 g of styrene, and 17.3 g of divinylbenzene and 0.26 g of azobisisobutyronitrile were used. Polymerization was performed to produce a porous body containing 50 mol% of a cross-linking component composed of a p-chloromethylstyrene / divinylbenzene copolymer. After separating 5 g of this porous material, adding 500 g of dioxane and heating at 80 ° C. for 30 minutes, the mixture was cooled to room temperature, 65 g of a trimethylamine (30%) aqueous solution was gradually added, and reacted at 50 ° C. for 3 hours. It was left overnight at room temperature. After completion of the reaction, the porous body was taken out, washed with acetone, washed with water, and dried to obtain a porous anion exchanger. The ion exchange capacity of this porous material was 2.5 mg equivalent / g in terms of dry porous material, and it was confirmed by SIMS that trimethylammonium groups were uniformly introduced into the porous material. Moreover, as a result of SEM observation, the internal structure of this porous body has an open cell structure, most of the macropores having an average diameter of 30 μm overlap, and the average diameter of the mesopores formed by the overlap of the macropores and the macropores. The value was 4 μm and the total pore volume was 9.9 ml / g. The porous body was cut out to a thickness of 10 mm, and the water permeation rate was measured. As a result, it was 12,000 l / min · m ² · MPa.

(Production of electric decation water production equipment)
An electric deionized water production apparatus having the following specifications as shown in the simplified diagram of FIG. 21 was used.
-Cell size: 160 ml (5 cm long x 4 cm wide x height (length between electrodes) 8 cm)
・ Cell container; internal volume 160ml
Anion exchange resin (filled on the anode side); 120 ml (IRA402BL), length 5 cm × width 4 cm × height 6 cm,
Cationic monolith: 5 cm long x 4 cm wide x 2 cm high cut from the monolith ion exchanger of Reference Example 2 in a wet state;
・ Treated water: Reverse osmosis membrane permeate, conductivity of about 20 μS / cm, flow rate of 15 l / hour ・ Electrode water: both anode water and cathode water, flow rate of 5 l / hour

(Operation of electric deionized water production equipment)
When the water to be treated was continuously passed through the obtained electric deionized water production apparatus at a flow rate of 15 l / hour (LV = 7.5, SV = 94 (whole)) and a direct current of 0.33 A was applied, The operating voltage was 56 V, and treated water having an electrical conductivity of 0.1 μS / cm was obtained. It was shown that pure water with high purity was produced by the electric deionized water production apparatus of the present invention. Moreover, the water flow differential pressure was 8.6 kPa. Moreover, when the inside of the container was observed during continuous operation, the anion exchange resin expanded and the cation monolith was crushed, and the mixed ion exchanger was in close contact with the container.

Comparative Example 1
(Production of electric decation water production equipment)
Instead of the monolith ion exchanger of Reference Example 2, an electric decationized water production apparatus was produced and operated in the same manner as in Example 1 except that the monolith ion exchanger of Reference Example 13 was used. . As in Example 1, the water to be treated was continuously passed through the electric deionized water production apparatus at a flow rate of 15 l / hour and a direct current of 0.33 A was applied. The operating voltage was 64 V, and the conductivity A treated water of 0.8 μS / cm was obtained. The water flow differential pressure was 67 kPa.

  The electric deionized water production apparatus of the present invention is used in various industries such as semiconductor manufacturing industry, pharmaceutical industry, food industry, power plant, laboratory, etc. using deionized water, or production of sugar solution, juice, wine, etc. Is done.

DESCRIPTION OF SYMBOLS 1 Cation exchange membrane 2 Anion exchange membrane 3a-3c Inlet 4a-4c Outlet 5a, 5b Communication pipe 6 Decation chamber 7 Deanion chamber 8 Nonconductor spacer 9 Cathode 10 Anode 11 Anion exchange resin 12 Cation exchange Resin 13 Cationic monolith 14 Anion monolith 15 Deionization chamber 20A-20C Electric deionized water production apparatus

Claims (8)

  A DC electric field is applied to the deionization chamber filled with the ion exchanger so that the ions to be excluded migrate in the same direction or the reverse direction with respect to the direction of water flow in the ion exchanger. In an electric deionized water production apparatus for removing adsorbed ionic impurities out of the system, the ion exchanger is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, and the monolithic organic The porous ion exchanger comprises an organic porous body composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or the organic porous body A composite structure with a large number of protrusions having a size of 4 to 40 μm formed on the surface of the skeleton, and having an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state The body in a wet state Electrodeionization water producing apparatus, characterized in that it is per ion exchange capacity 0.2mg equivalent / ml or more. A deanion chamber partitioned by an anion exchange membrane on one side and an ion exchange membrane on the other side, an anode disposed outside the anion exchange membrane on the one side, and an outer side of the ion exchange membrane on the other side And supplying water to be treated from the vicinity of the anion exchange membrane on one side in the deanion chamber, and from the vicinity of the ion exchange membrane on the other side in the deanion chamber. An anion cell for obtaining treated water;
A decation chamber partitioned by a cation exchange membrane on one side and an ion exchange membrane on the other side; a cathode disposed outside the cation exchange membrane on the one side; and an outer side of the ion exchange membrane on the other side The first treated water of the anion cell is supplied from the vicinity of one cation exchange membrane in the decation chamber, and the other ion exchange in the decation chamber is provided. Comprising a cation cell for obtaining the second treated water from the vicinity of the membrane,
Among the ion exchangers filled in the deanion chamber and decation chamber, at least one is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous ion The exchanger is an organic porous body composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or the skeleton surface of the organic porous body A composite structure with a large number of protrusions having a size of 4 to 40 μm, and having an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state, An electric deionized water production apparatus having an ion exchange capacity per volume of 0.2 mg equivalent / ml or more in a wet state of water. A decation chamber partitioned by a cation exchange membrane on one side and an ion exchange membrane on the other side; a cathode disposed outside the cation exchange membrane on the one side; and an outer side of the ion exchange membrane on the other side The first treatment is performed from the vicinity of the cation exchange membrane on the one side in the decation chamber by supplying water to be treated from the vicinity of the cation exchange membrane on the other side in the decation chamber. A cation cell for obtaining water;
A deanion chamber partitioned by an anion exchange membrane on one side and an ion exchange membrane on the other side, an anode disposed outside the anion exchange membrane on the one side, and an outer side of the ion exchange membrane on the other side The first treated water of the cation cell is supplied from the vicinity of the anion exchange membrane on one side in the deanion ion chamber, and the ion exchange on the other side in the deanion ion chamber is provided. Comprising an anion cell for obtaining the second treated water from the vicinity of the membrane,
At least one of the ion exchangers filled in the decation chamber and the deanion chamber is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous An organic porous body in which an ion exchanger is composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or a skeleton surface of the organic porous body It is a composite structure with a large number of protrusions having a size of 4 to 40 μm formed on the surface, and has an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state. An electric deionized water producing apparatus characterized by having an ion exchange capacity per volume of 0.2 mg equivalent / ml or more in a wet state of water.   The ion exchanger filled in the cation cell is a layered body in which a monolithic organic porous cation exchanger and a granular cation exchange resin phase are laminated in the direction of water flow, and the ion exchange filled in the anion cell. The electric deionized water production apparatus according to claim 2 or 3, wherein the body is a layered body in which a monolithic organic porous anion exchanger and a granular anion exchange resin phase are laminated in the direction of water flow. . An intermediate ion exchange membrane is provided between the anion exchange membrane on one side and the cation exchange membrane on the other side, and a deionization chamber partitioned by the one side anion exchange membrane and the intermediate ion exchange membrane, A decation chamber is defined by the cation exchange membrane on the other side and the intermediate ion exchange membrane, an anode outside the one side anion exchange membrane, and a cathode outside the cation exchange membrane on the other side The deionization cell is configured to supply water to be treated from the vicinity of the other cation exchange membrane in the decation chamber, and from the vicinity of the intermediate ion exchange membrane in the decation chamber. Treated water is obtained, the first treated water is supplied from the vicinity of one anion exchange membrane in the deanion chamber, and the second treated water is obtained from the vicinity of the intermediate ion exchange membrane in the deanion chamber. And
Among the ion exchangers filled in the deanion chamber and decation chamber, at least one is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous An organic porous body in which an ion exchanger is composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or a skeleton surface of the organic porous body It is a composite structure with a large number of protrusions having a size of 4 to 40 μm formed on the surface, and has an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state. An electric deionized water producing apparatus characterized by having an ion exchange capacity per volume of 0.2 mg equivalent / ml or more in a wet state of water. An intermediate ion exchange membrane between a cation exchange membrane on one side and an anion exchange membrane on the other side, and a decation chamber partitioned by the one side cation exchange membrane and the intermediate ion exchange membrane; A deanion chamber defined by the anion exchange membrane on the other side and the intermediate ion exchange membrane is configured, a cathode outside the cation exchange membrane on one side, and an anode outside the anion exchange membrane on the other side The deionization cell is configured to supply water to be treated from the vicinity of the anion exchange membrane on the other side in the deionization chamber, and from the vicinity of the intermediate ion exchange membrane in the deionization chamber. Treated water is obtained, the first treated water is supplied from the vicinity of one cation exchange membrane in the decation chamber, and the second treated water is obtained from the vicinity of the intermediate ion exchange membrane in the decation chamber. And
At least one of the ion exchangers filled in the decation chamber and the deanion chamber is a mixture of a monolithic organic porous ion exchanger and a granular ion exchange resin, the monolithic organic porous An organic porous body in which an ion exchanger is composed of a continuous skeleton phase and a continuous pore phase, a large number of particles having a diameter of 4 to 40 μm fixed to the skeleton surface of the organic porous body, or a skeleton surface of the organic porous body It is a composite structure with a large number of protrusions having a size of 4 to 40 μm formed on the surface, and has an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a wet state. An electric deionized water producing apparatus characterized by having an ion exchange capacity per volume of 0.2 mg equivalent / ml or more in a wet state of water.   The ion exchanger filled in the decation chamber is a layered body in which a monolithic organic porous cation exchanger and a granular cation exchange resin phase are laminated in the direction of water flow, and the deanion chamber is filled. 7. The apparatus for producing electrical deionized water according to claim 6, wherein the ion exchanger is a layered body in which a monolithic organic porous anion exchanger and a granular anion exchange resin phase are laminated in the direction of water flow. . A deionization chamber partitioned by an anion exchange membrane on one side and a cation exchange membrane on the other side, an anode disposed outside the anion exchange membrane on one side, and a cation exchange membrane on the other side A cathode disposed outside, supplying water to be treated from the vicinity of the anion exchange membrane on one side in the deionization chamber, and treating water from the vicinity of the other cation exchange membrane in the deionization chamber; Or water to be treated is supplied from the vicinity of the cation exchange membrane on the other side in the deionization chamber to obtain treated water from the vicinity of the anion exchange membrane on the one side in the deionization chamber. And
The ion exchanger filled in the deionization chamber was laminated with a monolithic organic porous anion exchanger, a granular anion exchange resin phase, and a monolithic organic porous cation exchanger from the anode side to the cathode side. A layered body or a layered body in which a granular anion exchange resin phase and a monolithic organic porous cation exchanger are laminated, the monolithic organic porous anion exchanger and the monolithic organic porous cation exchange 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 on the skeleton surface of the organic porous body or formed on the skeleton surface of the organic porous body A composite structure with a large number of protrusions having a size of 4 to 40 μm, having an average pore diameter of 10 to 150 μm and a total pore volume of 0.5 to 5 ml / g in a water-wet state. Per volume in state Electrodeionization water producing apparatus, characterized in that it is an ion exchange capacity 0.2mg equivalent / ml or more.