JP5282013B2 - Electric deionized water production system for fuel cells - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To provide an electric deionized water production apparatus which is excellent in heat-resisting properties of an anion exchanger filled in a desalting chamber and prevents voltage abnormality from occurring during operation. <P>SOLUTION: The electric deionized water production apparatus for a fuel cell which treats water recovered from a fuel cell includes the desalting chamber which is filled with the anion exchanger having a quaternary ammonium salt group represented by general formula (1) as an ion exchange group and a cation exchanger, and a positive plate and a negative plate provided parallel to each other so as to put the desalting chamber between them. <P>COPYRIGHT: (C)2011,JPO&amp;INPIT

Description

  The present invention relates to an electric deionized water production apparatus for a fuel cell.

  In recent years, fuel cells have attracted attention as power generation means that emits less carbon dioxide and has excellent environmental performance. In this fuel cell, energy generated when a reaction for generating water from hydrogen and oxygen is performed is extracted as electric power.

  During the operation of the fuel cell, heat is generated by the reaction of hydrogen and oxygen. For this reason, a circulating cooling water system is provided for cooling the fuel cell main body, and the fuel cell is cooled by circulating water therein. In addition, a reformer is provided at the front stage of the fuel cell, and hydrogen or the like is generated by steam reforming of the fuel, which is introduced into the fuel electrode (anode) of the fuel cell. Thus, water is used in the fuel cell.

  On the other hand, in a fuel cell, water vapor is generated from the air electrode (cathode) during power generation. Further, the cooling water flowing through the circulating cooling water system is a two-phase system of water vapor and water due to the heat generated when the fuel cell generates power. For this reason, these water vapor | steams are collect | recovered and condensed with a condenser, and it is set as water (Hereafter, this water may be described as "condensed water."). In order to reduce the amount of water used in the entire system, this condensed water is circulated and reused in the circulating cooling water system, the reformer, and the like.

  However, various anion components and cation components are dissolved in the condensed water. For this reason, in order to reuse the condensed water in the circulating cooling water system or the reformer, it is necessary to remove these ion components by water treatment. Thus, conventionally, water treatment apparatuses for removing ionic components in condensed water have been studied. Among these, the electrical deionized water production apparatus is useful because it has a high ionic component removal efficiency and can be used for a long time.

  In Patent Document 1 (Japanese Patent Laid-Open No. 2008-212871), Patent Document 2 (Japanese Patent Laid-Open No. 2008-161760) and Patent Document 3 (Japanese Patent Laid-Open No. 2008-161760), ion exchange is performed between an anode and a cathode. A pure water production apparatus having an electric deionized water production apparatus provided with at least a cathode side concentration chamber, a desalting chamber, and an anode side concentration chamber by disposing a membrane is disclosed. These electric deionized water production apparatuses are a mixed bed type in which the particulate anion exchanger and cation exchanger are mixed in the desalting chamber, or a stacked type in which layers are sequentially stacked in the direction of the condensed water flow. Filled.

JP 2008-212871 A JP 2008-161761 A JP 2008-161760 A

  The condensed water from the fuel cell is at a high temperature, and when the condensed water is processed by the electric deionized water production apparatus, this high-temperature condensed water passes through the demineralization chamber. However, in the electric deionized water production apparatuses of Patent Documents 1 to 3, the heat resistance of the particulate anion exchanger filled in the demineralization chamber has not been sufficiently considered. For this reason, when the condensed water passes through the desalting chamber, the anion exchanger filled in the desalting chamber may be deteriorated by heat, and the ion exchange capacity may be lowered.

In general, in an electric deionized water production apparatus, a water dissociation reaction occurs at the interface between the anion exchanger and the cation exchanger filled in the demineralization chamber. Hydrogen ions (H ⁺ ) and hydroxide ions (OH ⁻ ) generated by this water dissociation reaction form ionic bonds with the ion exchange groups of the cation exchanger and the anion exchanger, respectively. As a result, the cation exchanger and the anion exchanger are regenerated. Here, depending on the structure of the anion exchanger, the voltage at which this water dissociation reaction proceeds may be low.
However, in the electric deionized water production apparatuses of Patent Documents 1 to 3, since the types of anion exchangers are not sufficiently examined, the voltage necessary for the water dissociation reaction to increase is increased, and voltage abnormality occurs. There was a case.

  As described above, the conventional electric deionized water production apparatus has not sufficiently examined the heat resistance of the ion exchanger filled in the demineralization chamber and the prevention of voltage abnormality.

  The present invention has been made in view of the above problems. That is, an object of the present invention is to provide an electric deionized water production apparatus in which the anion exchanger filled in the desalting chamber is excellent in heat resistance and does not cause voltage abnormality during operation.

One embodiment is:
An electric deionized water production apparatus for a fuel cell for treating water recovered from the fuel cell,
A demineralization chamber filled with an anion exchanger having a quaternary ammonium base represented by the following general formula (1) as an ion exchange group, and a cation exchanger;
An anode plate and a cathode plate provided so as to be parallel to each other across the desalting chamber;
It is related with the electrical deionized water manufacturing apparatus provided with.

(However, in the general formula (1), at least one of R ^{1 to} R ³ represents an alkyl group having 2 or more carbon atoms, and X ⁻ represents a counter ion.)

  An anion exchanger filled in the desalting chamber is excellent in heat resistance, and an electric deionized water production apparatus that does not cause voltage abnormality can be provided.

It is a figure showing an example of the electrical deionized water manufacturing apparatus of this invention. It is a figure showing the electric deionized water manufacturing apparatus of 1st Example. It is a figure showing the electric deionized water manufacturing apparatus of 2nd Example. It is a figure showing the electric deionized water manufacturing apparatus of 3rd Example. It is a figure showing the electric deionized water manufacturing apparatus of 4th Example. It is a figure showing the electric deionized water manufacturing apparatus of 5th Example. It is a figure showing the electric power generating apparatus provided with the fuel cell and the electrical deionized water manufacturing apparatus. It is a figure showing the electric deionized water manufacturing apparatus of the comparative example 1.

1. Electric deionized water production device The electric deionized water production device is for a fuel cell that treats the water recovered from the fuel cell. Both sides of the demineralization chamber are sandwiched between the demineralization chamber and the demineralization chamber. And a cathode plate and an anode plate provided so as to be parallel to each other. The desalting chamber is filled with at least an anion exchanger having a quaternary ammonium base represented by the following general formula (1) as an ion exchange group and a cation exchanger.

(However, in the general formula (1), at least one of R ^{1 to} R ³ represents an alkyl group having 2 or more carbon atoms, and X ⁻ represents a counter ion).

  Thus, the anion exchanger filled in the desalting chamber has a quaternary ammonium base represented by the above general formula (1) as an ion exchange group, so that the anion exchanger has excellent heat resistance. It can be. Moreover, it is possible to prevent the occurrence of voltage abnormality during operation of the electric deionized water production apparatus.

  FIG. 1 is a drawing showing an example of an electrical deionized water production apparatus. As shown in FIG. 1, a desalting chamber 3 is provided between the anion exchange membrane 2a and the cation exchange membrane 2b. The desalting chamber 3 is filled with an anion exchanger 4 and a cation exchanger 1. The anode chamber 5 and the anode plate 7 are provided outside the anion exchange membrane 2a, and the cathode chamber 6 and the cathode plate 8 are provided outside the cation exchange membrane 2b. The anode plate 7 and the cathode plate 8 are connected to a DC power source (not shown). Condensed water flows in the direction of the arrow in the desalting chamber 3, and water flows in the direction of the arrow in the anode chamber 5 and the cathode chamber 6.

  While the condensed water flows through the desalting chamber 3, the anion component and the cation component in the condensed water are captured by the anion exchanger 4 and the cation exchanger 1, respectively. Then, a direct current is applied to the condensed water flowing through the desalting chamber 3 from the power source via the anode plate 7 and the cathode plate 8. Thereby, the anion component trapped by the anion exchanger 4 is electrophoresed and removed through the anion exchange membrane 2a to the anode chamber 5. Similarly, the cation component captured by the cation exchanger 1 is removed by electrophoretic migration to the cathode chamber 6 through the cation exchange membrane 2b. As described above, in the electric deionized water production apparatus, the ion component captured in the anion exchanger 4 and the cation exchanger 1 in the desalting chamber 3 by energizing between the electrodes, the anode chamber 5 and the cathode as needed. It is removed in the chamber 6.

Further, at the interface between the anion exchanger 4 and the cation exchanger 1 in the desalting chamber 3, hydrogen ions (H ⁺ ) and hydroxide ions (OH ⁻ ) are generated by water dissociation reaction. The anion exchanger 4 and the cation exchanger 1 are regenerated when these ions form an ionic bond with the anion exchanger 4 and the cation exchanger 1.

  As described above, in the electric deionized water production apparatus, it is possible to suppress a decrease in the ion exchange capacity due to the ion exchanger filled in the demineralization chamber, and it is possible to stably remove the ion component for a long time.

  In FIG. 1, the anode chamber 5 and the cathode chamber 6 may be provided with spacers or filled with an ion exchanger. When the ion exchanger is filled, the anode chamber 5 and the cathode chamber 6 may be in any form of a single bed of anion exchanger, a single bed of cation exchanger, or a mixed bed of anion exchanger and cation exchanger. . Thus, by filling the anode chamber 5 and the cathode chamber 6 with the ion exchanger, the electric resistance can be reduced.

  In FIG. 1, the flow of condensed water in the desalting chamber 3 and the flow of water in the anode chamber 5 and the cathode chamber 6 are in different directions. However, the flow direction of the water is not limited to this, and the flow direction of the condensed water in the desalting chamber 3 and the flow directions of the water in the anode chamber 5 and the cathode chamber 6 are the same. May be. The flow direction of water in the anode chamber 5 and the flow direction of water in the cathode chamber 6 are preferably the same.

  The electric deionized water production apparatus may have a structure in which one anode chamber / demineralization chamber / cathode chamber is provided between the anode plate and the cathode plate as shown in FIG. This type of electric deionized water production apparatus has, for example, a structure in which an anode plate / anode chamber / anion exchange membrane / anion exchange region / cation exchange region / cation exchange membrane / cathode chamber / cathode plate are arranged in this order. Can be mentioned. Moreover, as an electrical deionized water production apparatus, a structure in which an anode plate / anode chamber / anion exchange membrane / anion exchange region / intermediate ion exchange membrane / cation exchange region / cation exchange membrane / cathode chamber / cathode plate is arranged in this order. The thing which has can be mentioned. These types of electric deionized water production apparatuses can be used, for example, when treating water collected from a household fuel cell with a small amount of treated water. In this electric deionized water production apparatus, the configuration of the apparatus can be simplified and the cost can be reduced. Moreover, since the structure is simple, it is difficult to break down and maintenance is easy.

  Moreover, the electric deionized water production apparatus may provide a plurality of demineralization chambers and concentration chambers between the anode plate / anode chamber and the cathode chamber / cathode plate. That is, in this case, the electric deionized water production apparatus has a structure of anode plate / anode chamber / desalination chamber / concentration chamber / desalination chamber /.../ desalination chamber / cathode chamber / cathode plate. . The number of desalting chambers and concentration chambers provided between the anode plate / anode chamber and the cathode chamber / cathode plate is not particularly limited, and can be appropriately selected according to the required water treatment flow rate and treatment capacity. This type of electric deionized water production apparatus can be used when the amount of treated water is large.

  Hereinafter, (A) prevention of voltage abnormality during operation of the electric deionized water production apparatus and (B) improvement of heat resistance of the anion exchanger will be described in detail.

(A) Prevention of abnormal voltage occurrence At the interface between the anion exchanger and cation exchanger in the desalting chamber of the electric deionized water production apparatus, hydrogen ions (H ⁺ ) and hydroxide ions (OH ⁻ ) Occurs. These ions regenerate the anion exchanger and the cation exchanger by performing ionic bonds with the anion exchanger and the cation exchanger.

Here, in the anion exchanger having a quaternary ammonium base represented by the general formula (1), at least one of R ^{1 to} R ³ is an alkyl group having 2 or more carbon atoms. Thus, having a quaternary ammonium base having an alkyl group having 2 or more carbon atoms has a lower basicity than a case in which a lower molecular group such as a methyl group has a quaternary ammonium base bonded to a nitrogen atom. descend.

  On the other hand, the dissociation constant relating to the dissociation reaction (reversible reaction) of water represented by the following formula (A) is generally a value uniquely determined by the temperature.

  However, the dissociation constant of water is affected by the basicity of the anion exchanger and the value of the voltage applied to the water. Even at a constant temperature, the dissociation constant of water depends on the basicity of the anion exchanger and the value of the applied voltage. It is considered to change. That is, when the basicity of the anion exchanger decreases, the dissociation constant of water increases and the water dissociation reaction proceeds. Further, it is considered that the dissociation reaction of water proceeds when the voltage applied to water is increased.

  Therefore, the dissociation reaction of water can be promoted by using an anion exchanger having a quaternary ammonium base represented by the general formula (1) and having a low basicity as in the present invention. As a result, the water dissociation reaction can be caused to a desired level with a lower voltage / power. In contrast, in an anion exchanger having a quaternary ammonium base in which a low molecular group such as a methyl group is bonded to a nitrogen atom, the basicity is increased. For this reason, the dissociation constant of water becomes small, and in order to cause the water dissociation reaction to a desired level, it is necessary to increase the voltage applied to water. As a result, a voltage abnormality occurs.

(B) Improvement of heat resistance of anion exchanger The condensed water recovered from the fuel cell is at a high temperature. For this reason, when the heat resistance of the anion exchanger is low, the anion exchanger is deteriorated by high-temperature condensed water. In contrast, the anion exchanger filled in the desalting chamber of the present invention is excellent in heat resistance, and the ion exchange capacity of the anion exchanger does not deteriorate even when high-temperature condensed water is flowed into the desalting chamber. . For this reason, an electric deionized water manufacturing apparatus can be used stably for a long time.

For example, for a relatively small fuel cell system for home use, the “New Energy and Industrial Technology Development Organization” (hereinafter sometimes referred to as “NEDO”) constitutes each system that constitutes this system. Equipment standards are established. According to this standard, the maximum use temperature of condensed water is 50 ° C. Therefore, when using an electric deionized water production apparatus for a household fuel cell, it is necessary to conform to the above standard. The anion exchanger of the present invention can have a heat-resistant temperature of 50 ° C. or higher depending on the type of R ^{1 to} R ³ groups, and the electric deionized water production apparatus can be matched with the NEDO standard.

Further, for example, by making all of R ^{1 to} R ³ groups alkyl groups having 2 or more carbon atoms, heat resistance is higher than that of type II anion exchange resin (anion exchange resin having a dimethylethanolammonium group as an ion exchange group). It can be made excellent.

  Below, each part and material which comprise an electrical deionized water manufacturing apparatus are demonstrated.

(Anion exchanger)
The desalting chamber is filled with at least an anion exchanger having a quaternary ammonium base represented by the following general formula (1) as an ion exchange group.

(However, in the general formula (1), at least one of R ^{1 to} R ³ represents an alkyl group having 2 or more carbon atoms, and X ⁻ represents a counter ion).

In the general formula (1), R ^{1 to} R ³ are preferably each independently an alkyl group having 2 to 5 carbon atoms. R ^{1 to} R ³ are alkyl groups having 2 to 5 carbon atoms, so that an anion exchanger having more excellent anion exchange ability can be obtained, and occurrence of voltage abnormality can be effectively prevented.

In the general formula (1), R ^{1 to} R ³ are preferably ethyl groups. In this case, the quaternary ammonium base is a group represented by the following general formula (2).

Thus, by making all R < ¹ > -R < ³ > into an ethyl group, the maximum temperature which can use an anion exchanger stably is 75 degreeC, and it can be set as the thing excellent in heat resistance. Moreover, the anion exchange capacity of the anion exchanger can be made excellent. As such an anion exchange resin, PWA6 manufactured by Rohm and Haas can be used.

The anion X ⁻ of the general formula (2) is not particularly limited, but examples thereof include halide ions such as Cl ⁻ , Br ⁻ and I ⁻ , sulfate ions, NO ³⁻ , OH ⁻ , and p-toluenesulfone. Anions such as acid ions can be mentioned.

  The base structure of the anion exchanger is not particularly limited as long as it can add a quaternary ammonium base, and examples thereof include the following structures.

  Polymer materials constituting the matrix structure include styrene polymers such as polystyrene, poly (α-methylstyrene), and polyvinylbenzyl chloride; polyolefins such as polyethylene and polypropylene; poly (halogenated) such as polyvinyl chloride and polytetrafluoroethylene. Olefin); nitrile polymers such as polyacrylonitrile; (meth) acrylic polymers such as polymethyl methacrylate and polyethyl acrylate; styrene-divinylbenzene copolymer, vinylbenzyl chloride-divinylbenzene copolymer, etc. . The polymer may be a homopolymer obtained by polymerizing a single monomer, a copolymer obtained by polymerizing a plurality of monomers, or a blend of two or more polymers. . Among these organic polymer materials, styrene-divinylbenzene copolymer and vinylbenzyl chloride-divinylbenzene copolymer can be mentioned because of easy introduction of ion exchange groups and high mechanical strength.

  Although it does not specifically limit as an anion exchanger, The thing of the form of an anion exchange resin, an anion exchange membrane, an anion exchange fiber, and a monolithic anion exchanger can be used. Moreover, when using an anion exchange resin, either a gel form or MR form can be used.

  The desalting chamber may be filled with other anion exchangers in addition to the anion exchanger having the quaternary ammonium base represented by the above general formula (1) as an ion exchange group.

  As the monolithic anion exchanger, for example, those described in JP-A No. 2002-306976, JP-A No. 2009-062512, JP-A No. 2009-067982, and JP-A No. 2009-108294 can be used. .

  The anion exchanger described in JP-A-2002-306976 has an open-cell structure having macropores connected to each other and mesopores having an average diameter of 1-1000 μm in the walls of the macropores, and the total pore volume is 1 -50 ml / g, anion exchange groups are uniformly distributed, and the ion exchange capacity is 0.5 mg equivalent / g or more of a dry porous body. This anion exchanger has an open cell structure having mesopores having an average diameter of 1 to 1000 μm, preferably 10 to 100 μm in the macropores and the walls of the macropores connected to each other. These open cells usually have macropores and macropores having an average diameter of 2 to 5000 μm, and these overlapping portions have mesopores that form a common opening, and most of them have an open pore structure. The number of overlapping macropores is 1 to 12 for one macropore, and 3 to 10 for many. By using the anion exchanger as described above, elasticity is high, and shape change due to swelling or shrinkage can be suppressed. In addition, the operating voltage can be stabilized, and deformation of the cation exchanger filled in the desalting chamber can be prevented.

  The anion exchanger described in JP 2009-062512 A is a continuous macropore structure in which bubble-shaped macropores overlap each other, and the overlapping portion becomes an opening having an average diameter of 30 to 300 μm in a wet state of water, and has a thickness of 1 mm. As described above, the total pore volume is 0.5 to 5 ml / g, the ion exchange capacity per volume in a water-wet state is 0.4 mg equivalent / ml or more, and the anion exchange groups are uniformly distributed in the porous anion exchanger. In addition, in the SEM image of the cut surface of the continuous macropore structure (dried body), the skeleton part area appearing in the cross section may be 25 to 50% in the image region. This anion exchanger has a continuous macropore structure in which bubble-shaped macropores overlap each other, and the overlapping portion becomes an opening (mesopore) having an average diameter of 30 to 300 μm, preferably 30 to 200 μm, particularly 35 to 150 μm. The skeleton area is preferably 25 to 45% in the image area, and the ion exchange capacity is preferably 0.4 to 1.8 mg equivalent / ml.

  As the anion exchanger described in JP-A-2009-067982, a thick polymer composed of an aromatic vinyl polymer containing 0.3 to 5.0 mol% of a crosslinked structural unit among all the structural units into which an anion exchange group has been introduced. A co-continuous structure comprising a three-dimensionally continuous skeleton having a diameter of 1 to 60 μm and three-dimensionally continuous pores having a diameter of 10 to 100 μm between the skeletons, and the total pore volume is 0 .5-5 ml / g, ion exchange capacity per volume in a water-wet state is 0.3 mg equivalent / ml or more, and anion exchange groups are uniformly distributed in the porous anion exchanger Can be mentioned. This anion exchanger has a three-dimensional continuous skeleton having an anion exchange group introduced with a thickness of 1 to 60 μm, preferably 3 to 58 μm, and a diameter of 10 to 100 μm, preferably 15 to 90 μm between the skeletons. In particular, it has a co-continuous structure composed of three-dimensionally continuous pores of 20 to 80 μm. The ion exchange capacity is preferably 0.4 to 1.8 mg equivalent / ml.

  As the anion exchanger described in JP-A-2009-108294, an organic porous body composed of a continuous skeleton phase and a continuous pore phase, and a large number of 4 to 40 μm in diameter fixed to the skeleton surface of the organic porous body. A composite structure with a large number of protrusions having a maximum diameter of 4 to 40 μm formed on the skeleton surface of the particle body or the organic porous body, and having a thickness of 1 mm or more, an average diameter of pores of 10 to 150 μm, Examples are those having a pore volume of 0.5 to 5 ml / g, an ion exchange capacity of 0.2 mg equivalent / ml or more per volume in a wet state of water, and an anion exchange group uniformly distributed in the composite structure. be able to. As this organic porous body, two types of organic porous bodies can be used. The first organic porous body constitutes 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 300 μm, preferably 30 to 200 μm, particularly 35 to 150 μm. To do. The second organic porous body constitutes a co-continuous structure having a three-dimensionally continuous skeleton having a diameter of 1 to 50 μm and a three-dimensionally continuous pore having a diameter of 10 to 100 μm between the skeletons.

  By using the anion exchanger described in JP 2009-062512 A, JP 2009-067982 A, and JP 2009-108294 A, the conductivity in the demineralization chamber is increased, and electric deionization is performed. The operating voltage of the water production apparatus can be lowered.

In addition to the monolithic anion exchanger described in the above publication, the following monolithic anion exchanger can be used. That is, the monolithic anion exchanger is a continuous macropore structure having a thickness of 1 mm or more in which bubble-shaped macropores overlap each other, and the overlapping portion becomes an opening having an average diameter of 20 to 200 μm, and the skeleton of the continuous macropore structure The surface layer part of the part has a porous structure, and has an ion exchange capacity of 0.4 mg equivalent / ml or more per volume in a water-wet state, and anion exchange groups are uniformly distributed in the porous anion exchanger. The average diameter of the overlapping portion is preferably 20 to 150 μm, and more preferably 20 to 100 μm. Moreover, 30-300 micrometers is preferable in the water wet state, as for the average diameter of this overlapping part, 30-200 micrometers is more preferable, and 35-150 micrometers is still more preferable. The specific surface area of the monolithic anion exchanger is preferably 20m ² / g~70m ² / g. The thickness of the monolithic anion exchanger is preferably 3 mm to 1000 mm. The ion exchange capacity per volume of the monolithic anion exchanger in the water-wet state is preferably 0.4 to 1.8 mg equivalent / ml.

(Cation exchanger)
Although it does not specifically limit as a cation exchanger, A cation exchange membrane, a cation exchange fiber, a monolithic cation exchanger, and a cation exchange resin can be used. When a cation exchange resin is used, either gel form or MR form can be used. The monolithic cation exchanger can be produced by a production method similar to the production method of the monolithic anion exchanger described above (anion exchanger).

(Desalination room)
When the intermediate ion exchange membrane is not provided, the desalting chamber is composed of a cation exchange membrane, an anion exchange membrane, and a frame. Moreover, when providing an intermediate ion exchange membrane, the desalting chamber is comprised from the cation exchange membrane, the anion exchange membrane, the intermediate ion exchange membrane, and the frame.

  The frame is composed of ribs having hollow interior spaces. A cation exchange membrane and an anion exchange membrane are disposed on one side and the other side of the frame, respectively. Moreover, when providing an intermediate ion exchange membrane, the intermediate ion exchange membrane is arrange | positioned in the center of a frame. The internal space of this frame is filled with anion exchangers and cation exchanges. At least a part of this anion exchanger is composed of an anion exchanger having a quaternary ammonium base represented by the above general formula (1) as an ion exchange group. In addition to the anion exchanger having the quaternary ammonium base represented by the general formula (1), other anion exchangers may be filled as the anion exchanger.

  In the desalting chamber, the boundary surface between the cation exchange region filled with the cation exchanger and the anion exchange region filled with the anion exchanger is preferably parallel to the cathode plate and the anode plate. By making the boundary surface parallel to the cathode plate and the anode plate in this way, the ion exchange regions can be arranged in the order of anion exchange region / cation exchange region from the anode plate side to the cathode plate side ( In the above, “/” corresponds to the boundary surface).

  As a result, when the desalination chamber is energized, not only the occurrence of voltage abnormality can be prevented, but also the deterioration of treated water can be effectively prevented. That is, in general, the anion exchanger and the cation exchanger filled in the desalting chamber have different conductivity. Therefore, for example, when the anion exchanger and the cation exchanger are filled in the desalting chamber in order along the flow direction of the condensed water (for example, the inlet side-anion exchanger-cation exchange with respect to the flow direction of the condensed water). The interface between the anion exchange region and the cation exchange region is formed between the cathode plate and the anode plate. It becomes perpendicular to it. In this case, a current flows through an ion exchanger having excellent conductivity among the anion exchanger and the cation exchanger. And in the part of the ion exchanger where an electric current does not flow easily, the efficiency of ion exchange is lowered, and the quality of treated water may be lowered.

  On the other hand, when the boundary surface between the cation exchange region and the anion exchange region is provided in parallel to the cathode plate and the anode plate, the current flows through both the cation exchange region and the anion exchange region during energization. Will flow. Therefore, in this case, no current flows through any one of the ion exchangers, and it is possible to prevent deterioration of the treated water quality. The boundary surface between the cation exchange region and the anion exchange region may be substantially parallel to the anode plate and the cathode plate, and does not need to be strictly parallel to the anode plate and the cathode plate. .

  “Anion exchange region” refers to a region occupied by an anion exchanger filled in a desalting chamber. With respect to the particulate anion exchange resin, the region filled with the particulate anion exchange resin in the desalting chamber constitutes the anion exchange region. When a plurality of anion exchangers are filled in the desalting chamber, a region occupied by all the anion exchangers becomes an “anion exchange region”.

  Similarly, the “cation exchange region” represents a region occupied by the cation exchanger filled in the desalting chamber. Regarding the particulate cation exchange resin, the region filled with the particulate cation exchange resin in the desalting chamber constitutes the cation exchange region. When a plurality of cation exchangers are filled in the desalting chamber, a region occupied by all the cation exchangers is a “cation exchange region”.

In addition, the “boundary surface” represents a surface constituting a boundary portion between the anion exchange region and the cation exchange region. For example, when both an anion exchanger and a cation exchanger are constituted by an ion exchange membrane, an ion exchange fiber, and a monolithic ion exchanger, a surface where the anion exchanger and the cation exchanger are in contact constitutes a boundary surface.
When either anion exchanger or cation exchanger is particulate ion exchange resin and the other is ion exchange membrane, ion exchange fiber, monolithic ion exchanger, ion exchange membrane, ion exchange fiber, monolithic ion exchange The surface of the body facing the particulate ion exchange resin substantially constitutes the boundary surface.
When both an anion exchanger and a cation exchanger are composed of a particulate ion exchange resin, an intermediate membrane is disposed at the boundary between the anion exchange region and the cation exchange region, and this intermediate membrane constitutes the boundary surface.

(Anode plate and cathode plate)
Although it does not specifically limit as a material of an anode plate, Since chlorine may generate | occur | produce at the time of operation | movement of an electrical deionized water manufacturing apparatus, what has chlorine resistance is preferable. As a material of the anode plate, for example, a noble metal such as platinum, palladium, iridium, or a net-like or plate-like electrode in which these noble metals are coated with titanium or the like can be used.

  The material of the cathode plate is not particularly limited as long as it functions as a cathode. For example, plate-like stainless steel or mesh-like stainless steel can be used.

  Note that the anode plate and the cathode plate may be disposed so as to be substantially parallel, and may not be disposed so as to be strictly parallel.

2. Power Generation Device FIG. 7 is a diagram illustrating an example of a power generation device including the electric deionized water production device of the present invention. As shown in FIG. 7, this power generator includes a fuel cell having a fuel electrode 21, an electrolyte membrane 24, an air electrode 25, and a cooling unit 29. During power generation by the fuel cell, water vapor is generated from the air electrode 25 and the cooling unit 29.

  These water vapors are collected and condensed by the condenser 23 to become condensed water. This condensed water is introduced into the electric deionized water production apparatus 26, and the anion component and the cation component are removed.

  The condensed water treated by the electric deionized water production apparatus 26 is cooled by the treatment tank 28 to become cooling water. This cooling water is supplied to the cooling unit 29 and is also supplied to the front part of the reformer 22 and mixed with the fuel gas. The cooling water mixed with the fuel gas is introduced into the reformer 22. In the reformer 22, steam reforming of the fuel gas is performed to generate hydrogen. Hydrogen produced in the reformer 22 is introduced into the fuel electrode 21 of the fuel cell. On the other hand, air is introduced into the air electrode 25 of the fuel cell. The fuel cell generates electric power by the reaction between hydrogen introduced into the fuel electrode 21 and oxygen in the air introduced into the air electrode 25.

  The water vapor generated in the air electrode 25 and the cooling unit 29 is condensed as described above, then regenerated in the electric deionized water production apparatus 26, and then reused.

  In addition, in the said electric power generating apparatus, the fuel cell of 1 cell was shown notionally. However, a fuel cell in the form of a cell stack in which a plurality of cells are stacked via separators may be used according to the required power generation amount. Moreover, the kind of fuel cell to be used is not particularly limited, and a polymer electrolyte fuel cell (PEFC), a phosphoric acid fuel cell (PAFC), a molten carbonate fuel cell (PAFC, Phosphoric Acid Fuel Cell) MCFC, Molten Carbonate Fuel Cell), solid oxide fuel cell (SOFC), alkaline electrolyte fuel cell (AFC), Alkaline Fuel Cell, etc. can be used. In the case of an internal reforming type fuel cell, cooling water is supplied directly into the fuel cell without providing a reformer.

  In the power generator, the condensed water obtained by condensing the water vapor collected from the air electrode 25 and the cooling unit 29 is at a high temperature. Therefore, in the conventional electric deionized water production apparatus, the anion exchanger in the demineralization chamber may be deteriorated by high-temperature condensed water. However, in this power generation device, since the anion exchanger filled in the demineralization chamber of the electric deionized water production apparatus has the ion exchange group represented by the general formula (1), it has excellent heat resistance. For this reason, the anion component in condensed water can be removed stably for a long time. Further, since this anion exchanger is present, the dissociation reaction of water can be promoted at a low voltage, and the occurrence of voltage abnormality can be prevented.

  Hereinafter, a specific example of the electric deionized water production apparatus will be described. In the following first to fifth examples, the anion exchanger is an anion exchanger having a quaternary ammonium base represented by the general formula (1) as an ion exchange group.

  In addition, the following specific examples are specific examples shown for a deeper understanding of the present invention, and the present invention is not limited to these specific examples. In the following specific examples, for convenience, the description will be divided into a plurality of embodiments. However, except where explicitly stated and in principle impossible, they are not independent of each other, one being in the relationship of some or all of the other.

(First embodiment)
FIG. 2 is a diagram showing an electric deionized water production apparatus according to this embodiment. As shown in FIG. 2, in this electric deionized water production apparatus, an anion exchange region 15 / particulate cation exchange resin 10 comprising an anode plate 7 / anode chamber 5 / anion exchange membrane 2a / monolithic anion exchanger 11 is provided. The filled cation exchange region 16 / cation exchange membrane 2b / cathode chamber 6 / cathode plate 8 are arranged in this order. The desalting chamber 3 is filled with a monolithic anion exchanger 11 and a particulate cation exchange resin 10.

  In the desalting chamber 3, the region occupied by the monolithic anion exchanger 11 constitutes the anion exchange region 15. In the desalting chamber 3, a region filled with the particulate cation exchange resin 10 constitutes a cation exchange region 16. A boundary surface 14 between the anion exchange region 15 and the cation exchange region 16 is parallel to the anode plate 7 and the cathode plate 8. That is, in the present embodiment, the surface on the cathode side (surface facing the cathode plate 8) of the monolithic anion exchanger 11 substantially constitutes the boundary surface 14.

  In the present embodiment, the use of the monolithic anion exchanger 11 makes it easy to control the boundary surface 14 to be parallel to the anode plate 7 and the cathode plate 8. As a result, the current flow in the desalting chamber is less likely to be biased when energized, and the deterioration of the treated water can be effectively prevented. Moreover, since the anion exchanger having the quaternary ammonium base represented by the general formula (1) is used, it is possible to prevent the occurrence of voltage abnormality and improve the heat resistance.

  In addition, since the configuration of the apparatus is simple, cost reduction can be achieved. Further, during normal operation, in the conventional electric deionized water production apparatus, the filling state of the particulate cation exchange resin may become non-uniform with the generation / stop of the water flow into the demineralization chamber. However, in this embodiment, by providing the monolithic anion exchanger 11 in the desalting chamber 3, the filling state of the particulate cation exchange resin 10 is fixed, and the filling state is prevented from becoming uneven. be able to.

(Second embodiment)
FIG. 3 is a diagram showing an electric deionized water production apparatus according to this embodiment. As shown in FIG. 3, in this electric deionized water production apparatus, anion plate 7 / anode chamber 5 / anion exchange membrane 2a / anion exchange region 15 filled with particulate anion exchange resin 13 / monolithic cation exchanger 12 are arranged in the order of cation exchange region 16 / cation exchange membrane 2b / cathode chamber 6 / cathode plate 8. The desalting chamber 3 is filled with a monolithic cation exchanger 12 and a particulate anion exchange resin 13.

  In the desalting chamber 3, a region occupied by the monolithic cation exchanger 12 constitutes a cation exchange region 16. In the desalting chamber 3, the region filled with the particulate anion exchange resin 13 constitutes the anion exchange region 15. The boundary surface 14 between the anion exchange region 15 and the cation exchange region 16 is parallel to the anode plate 7 and the cathode plate 8. That is, in this embodiment, the surface on the anode side (surface facing the anode plate 7) of the monolithic cation exchanger 12 substantially constitutes the boundary surface 14.

  In the present embodiment, the use of the monolithic cation exchanger 12 makes it easy to control the boundary surface 14 in parallel with the anode plate 7 and the cathode plate 8, and can effectively prevent deterioration of the treated water quality. Moreover, since the anion exchanger having the quaternary ammonium base represented by the general formula (1) is used, it is possible to prevent the occurrence of voltage abnormality and improve the heat resistance.

  In addition, since the configuration of the apparatus is simple, cost reduction can be achieved. Furthermore, by providing the monolithic cation exchanger 12 in the desalting chamber 3, the filling state of the particulate anion exchange resin 13 can be fixed, and the filling state can be prevented from becoming uneven.

(Third embodiment)
FIG. 4 is a diagram showing an electrical deionized water production apparatus according to the present embodiment. As shown in FIG. 4, in this electric deionized water production apparatus, from the anion exchange region 15 / monolithic cation exchanger 12 comprising anode plate 7 / anode chamber 5 / anion exchange membrane 2a / monolithic anion exchanger 11 The cation exchange region 16 / the cation exchange membrane 2b / the cathode chamber 6 / the cathode plate 8 are arranged in this order. The desalting chamber 3 is filled with a monolithic anion exchanger 11 and a monolithic cation exchanger 12.

  In the desalting chamber 3, the region occupied by the monolithic anion exchanger 11 constitutes the anion exchange region 15. In the desalting chamber 3, a region occupied by the monolithic cation exchanger 12 constitutes a cation exchange region 16. A boundary surface 14 between the anion exchange region 15 and the cation exchange region 16 is parallel to the anode plate 7 and the cathode plate 8. That is, in the present embodiment, the surface where the monolithic anion exchanger 11 and the monolithic cation exchanger 12 substantially contact each other constitutes the boundary surface 14.

  In this embodiment, by using the monolithic anion exchanger 11 and the monolithic cation exchanger 12, it is very easy to make the boundary surface 14 parallel to the anode plate 7 and the cathode plate 8. As a result, it is possible to more effectively prevent deterioration of treated water quality. Moreover, since the anion exchanger having the quaternary ammonium base represented by the general formula (1) is used, it is possible to prevent the occurrence of voltage abnormality and improve the heat resistance.

  In addition, since the configuration of the apparatus is simple, cost reduction can be achieved. Furthermore, since there is no particulate ion exchange resin in the desalting chamber 3, the filling state of the particulate ion exchange resin does not become uneven with the generation / stop of the flow of water into the desalting chamber.

(Fourth embodiment)
FIG. 5 is a diagram showing an electric deionized water production apparatus according to the present embodiment. As shown in FIG. 5, in this electric deionized water production apparatus, anode plate 7 / anode chamber 5 / anion exchange membrane 2a / anion exchange region 15 filled with particulate anion exchange resin 13 / intermediate ion exchange membrane 17 / Cation exchange region 16 filled with particulate cation exchange resin 10 / cation exchange membrane 2b / cathode chamber 6 / cathode plate 8 are arranged in this order. This intermediate ion exchange membrane 17 constitutes the boundary surface 14.

  Generally, when filling the desalination chamber with the particulate anion exchange resin and the particulate cation exchange resin, it is difficult to make the interface parallel to the anode plate and the cathode plate. In addition, due to the occurrence / stop of the flow of water into the desalting chamber, the filling state of the particulate anion exchange resin and the particulate cation exchange resin filled in the desalting chamber changes, and the boundary surface becomes uncertain, May change. However, in this embodiment, by providing the intermediate ion exchange membrane 17 in the desalting chamber 3, the region filled with the particulate anion exchange resin 13 and the particulate cation exchange resin 10 can be partitioned. As a result, the portion of the intermediate ion exchange membrane 17 can be defined as the boundary surface 14. And it becomes easy to arrange the boundary surface 14 in parallel with respect to the anode plate 7 and the cathode plate 8. Moreover, it becomes easy to prevent the fall of treated water quality more effectively.

  The intermediate ion exchange membrane 17 may be either a single membrane of a cation exchange membrane or an anion exchange membrane, or a dual membrane in which both an anion exchange membrane and a cation exchange membrane are arranged. The dual membrane is, for example, an anion exchange membrane that occupies a certain area in a plane perpendicular to the thickness direction, such as when the upper half is an anion exchange membrane and the lower half is a cation exchange membrane, and the remaining area Represents a membrane occupied by a cation exchange membrane.

  In the electric deionized water production apparatus of this embodiment, water can be separately passed through the anion exchange region 15 and the cation exchange region 16. The order of water flow to these ion exchange regions is not particularly limited, and water may flow in the order of anion exchange region 15 → cation exchange region 16 or water in the order of cation exchange region 16 → anion exchange region 15. good.

  Below, the method of using an electric deionized water production apparatus will be described by taking as an example a case where water is passed in the order of the cation exchange region 16 → the anion exchange region 15.

  As shown in FIG. 5, the condensed water first flows in the cation exchange region 16, during which cation components in the condensed water are removed. Thereafter, the condensed water flows in the anion exchange region 15, and during this time, anion components in the condensed water are removed. In addition, water flows into the anode chamber 5 and receives an anionic component that is electrophoresed through the anion exchange membrane 2a. Similarly, water flows into the cathode chamber 6 and receives a cation component that migrates electrically via the cation exchange membrane 2b.

  In the present embodiment, since the cation component is first removed in the cation exchange region 16, the anion component remains in the condensed water, and hydrogen ions generated by the water dissociation reaction as these counter ions increase in the condensed water. . As a result, the pH of the condensed water after removal of the cation component becomes closer to acidity (for example, pH 5 to 6). Therefore, after this, the condensed water flowing into the anion exchange region 15 becomes acidic, and the amount of hydroxide ions, which are anion components that easily migrate in the condensed water, decreases. As a result, it becomes easy to remove anion components other than hydroxide ions in the condensed water. Thus, the electric deionized water production apparatus of the present embodiment can obtain high-purity water.

  Hereinafter, the function of the intermediate ion exchange membrane 17 when water is passed in the order of the cation exchange region 16 and the anion exchange region 15 will be described.

  When a single cation exchange membrane is used as the intermediate ion exchange membrane 17, cation components that cannot be completely removed in the cation exchange region 16 and are present in the condensed water flowing through the anion exchange region 15 are removed from the cation exchange membrane (intermediate ion exchange membrane 15). It can be removed again via the (exchange membrane) 17. As a result, the anion component removal performance can be improved.

  When a single membrane of an anion exchange membrane is used as the intermediate ion exchange membrane 17, while the condensed water flows in the cation exchange region 16, the anion component in the condensed water passes through the anion exchange membrane (intermediate ion exchange membrane) 17. Migrate through the anion exchange region 15. Thereby, the removal efficiency of the anion component can be increased. In addition, the pH of the condensed water in the cation exchange region 16 changes from acidic to slightly neutral, and the removal efficiency of the cation component in the vicinity of the end of the cation exchange region 16 can be further increased.

  When a dual membrane of anion exchange membrane and cation exchange membrane is used as the intermediate ion exchange membrane 17, both when using a single membrane of the cation exchange membrane and when using a single membrane of the anion exchange membrane You can combine benefits.

  In FIG. 5, the flow of condensed water in the cation exchange region 16 and the anion exchange region 15 is in the same direction. However, the flow direction of water is not limited to this, and the flow direction of the condensed water in the cation exchange region 16 and the flow direction of the condensed water in the anion exchange region 15 are different even if they are opposite. Also good.

(5th Example)
FIG. 6 is a diagram showing a modification of the first embodiment. As shown in FIG. 6, in this electric deionized water production apparatus, the desalting chamber 3 and the concentration chamber 18c are alternately arranged between the anode plate 7 / anode chamber 18a and the cathode chamber 18b / cathode plate 8. This is different from the first embodiment in that it constitutes the structure. The desalting chamber 3 is arranged in the order of anion exchange membrane 2a / anion exchange region 15 / cation exchange region 16 / cation exchange membrane 2b from the anode side to the cathode side. A boundary surface 14 exists in each desalting chamber 3. Since the electrical deionized water production apparatus of the present embodiment is provided with a plurality of demineralization chambers and concentration chambers, the ion exchange capacity in the condensed water can be enhanced.

  The concentration chamber 18c may be filled with an ion exchanger as in the anode chamber 18a and the cathode chamber 18b. In this case, the concentration chamber 18c may be in any form of a single bed of anion exchanger, a single bed of cation exchanger, or a mixed bed of anion exchanger and cation exchanger.

  In the present embodiment, an example in which a plurality of desalting chambers and concentration chambers are provided as a modification of the first embodiment has been described. However, the structure in which a plurality of demineralization chambers and concentration chambers are provided is not limited to the modification of the first embodiment. In the electric deionized water production apparatus of the second to fourth embodiments, As described above, a plurality of desalting chambers and concentration chambers may be provided.

  In the first to fifth embodiments, in addition to the anion exchanger having the quaternary ammonium base represented by the general formula (1) as an ion exchange group in the anion exchange region, other anion exchangers are used. May be filled.

Example 1
An electric deionized water production apparatus shown in FIG. 5 was prepared. As the particulate anion exchange resin 13, PWA6 (manufactured by Rohm and Haas) having a quaternary ammonium base represented by the general formula (2) as an ion exchange group was used. Moreover, IR120B (made by Rohm and Haas) was used for the particulate cation exchange resin 10, and a cation exchange membrane (made by Astom) was used for the intermediate ion exchange membrane 17.

  After placing the intermediate ion exchange membrane 17 in the center of the desalting chamber 3, 80 mL of the particulate anion exchange resin 13 and 80 mL of the particulate cation exchange resin 10 were filled. The volumes of the particulate anion exchange resin 13 and the particulate cation exchange resin 10 were measured by a tapping method. The size of the anode plate 7 and the cathode plate 8 was 10 cm long and 10 cm wide.

  UPW (ultra pure water, temperature 25 ° C., conductivity 0.1 μS / cm) was first flowed to the cation exchange region 16 of the desalting chamber and then to the anion exchange region 15 at a flow rate of 4 L / h. The direction in which UPW flows through the anion exchange region 15 and the cation exchange region 16 was the same direction.

  Further, UPW (ultra pure water, temperature 25 ° C., conductivity 0.1 μS / cm) was passed through the anode chamber 5 and the cathode chamber 6 at a flow rate of 4 L / h. The direction in which UPW flows through the anode chamber 5 and the cathode chamber 6 was opposite to the direction in which condensed water flows through the anion exchange region 15 and the cation exchange region 16. Then, currents of 0.20 A and 1.0 A were passed between the anode plate 7 and the cathode plate 8, and the voltage in the region 20 when 2 hours passed was measured. The results are shown in Table 1.

(Example 2)
An electric deionized water production apparatus shown in FIG. 2 was prepared. The test was conducted in the same manner as in Example 1 except that 80 mL of the monolithic anion exchanger 11 was filled in the anion exchange region as the anion exchanger. The volume of the monolithic anion exchanger 11 was measured as the volume occupied by the outer portion of the monolithic anion exchanger 11.

  This monolithic anion exchanger 11 has a quaternary ammonium base represented by the above general formula (2) as an ion exchange group. Moreover, the average diameter of the opening part of the monolithic anion exchanger 11 is 62 μm, the total pore volume is 2.39 ml / g, the ion exchange amount is 0.50 mg equivalent / g, and the wet porous body (3.2 mg equivalent / g). The dry porous body) had a moisture retention capacity of 84%, 1.3 mol% of crosslinked structural units, and a skeleton area per unit cross-sectional area of 30%.

  Thereafter, the voltage in the region 20 was measured in the same manner as in Example 1. The results are shown in Table 1.

(Comparative Example 1)
As shown in FIG. 8, the test was conducted in the same manner as in Example 1 except that 80 mL of particulate anion exchange resin 19 IRA402BL (Rohm and Haas) was filled in the anion exchange region as an anion exchanger. It was. This particulate anion exchange resin 19 does not have a quaternary ammonium base represented by the general formula (1) as an ion exchange group. Thereafter, the voltage in the region 20 was measured in the same manner as in Example 1. The results are shown in Table 1.

  As shown in Table 1, in Example 1, the voltage was 1V at a current of 0.2A, the voltage was 2V at a current of 1.0A, and the voltage value was small in both cases of the currents of 0.2A and 1.0A. . Similarly, in Example 2, the voltage is 1.5 V at a current of 0.2 A and the voltage is 2.5 V at a current of 1.0 A, and the voltage value is small in both cases of the currents of 0.2 A and 1.0 A. It was.

  On the other hand, in Comparative Example 1, the voltage was 4 V at a current of 0.2 A, and the voltage was 45 V at 1.0 A, and the voltage value showed a large value in both cases of the currents of 0.2 A and 1.0 A.

  As described above, when the current is 0.2 A or 1.0 A, the voltage value is larger in Comparative Example 1 than in Examples 1 and 2, and it is understood that a voltage abnormality has occurred. .

  In the above examples and comparative examples, the voltage value when UPW was passed through the desalting chamber was examined. However, the condensed water from the fuel cell contains a larger amount of ionic components than UPW, so the conductivity of the condensed water is higher than UPW. Therefore, it is considered that the voltage value is larger when the condensed water is flowed into the desalting chamber than when the UPW is flowed into the desalting chamber, and the voltage abnormality is more remarkable in Comparative Example 1. .

  Moreover, since the heat-resistant temperature of PWA6 (made by Rohm and Haas) used in Example 1 and the monolithic anion exchanger used in Example 2 is 75 ° C., high-temperature condensed water is allowed to flow into the desalting chamber. Even in this case, the anion exchanger does not deteriorate.

  As described above, the anion exchanger having the quaternary ammonium base represented by the above general formula (1) as the ion exchange group is filled in the desalting chamber, so that the heat resistance is excellent and the operation voltage is lowered and stable. It was confirmed that the operation of the electric deionized water production apparatus was possible.

  The electric deionized water production apparatus of the present invention can be used in an electric deionized water production apparatus for a fuel cell that processes water recovered from the fuel cell. In particular, it can be suitably used as an electric deionized water production apparatus for household fuel cells.

1 Cation Exchanger 2a Anion Exchange Membrane 2b Cation Exchange Membrane 3 Desalination Chamber 4 Anion Exchanger 5 Anode Chamber 6 Cathode Chamber 7 Anode Plate 8 Cathode Plate 10 Particulate Cation Exchange Resin 11 Monolithic Anion Exchanger 12 Monolithic Cation Exchanger 13 particulate anion exchange resin 14 interface 15 anion exchange region 16 cation exchange region 17 intermediate ion exchange membrane 18a anode chamber 18b cathode chamber 18c concentration chamber 19 particulate anion exchange resin 21 fuel electrode 22 reformer 23 condenser 24 ion exchange Membrane 25 Air electrode 26 Electric deionized water production device 28 Treatment tank 29 Cooling section

Claims (5)

An electric deionized water production apparatus for a fuel cell for treating water recovered from the fuel cell,
A demineralization chamber filled with an anion exchanger having a quaternary ammonium base represented by the following general formula ( 2 ) as an ion exchange group, and a cation exchanger;
An anode plate and a cathode plate provided so as to be parallel to each other across the desalting chamber;
An electrical deionized water production apparatus comprising:

In the desalting compartment, and the cation exchange region cation exchanger is filled, the interface of the anion exchange area anion exchanger is filled, according to claim 1 which is parallel to the anode plate and cathode plate Electric deionized water production equipment. The electric deionized water production apparatus according to claim 2 , wherein the desalting chamber is filled with the cation exchanger and the anion exchanger so as to be in any one of the following forms (a) to (c). .
(A) the cation exchanger is a monolithic cation exchanger, the anion exchanger is a particulate anion exchange resin,
(B) the cation exchanger is a particulate cation exchange resin, the anion exchanger is a monolithic anion exchanger,
(C) The cation exchanger is a monolithic cation exchanger, and the anion exchanger is a monolithic anion exchanger. The electrodeionization water producing apparatus according to claim 2 or 3 having an order arranged structure of the anode plate / anode compartment / anion exchange membrane / anion exchange region / cation exchange area / cation exchange membrane / cathode chamber / cathode plate The electrical deionized water production apparatus according to 1. The electric deionized water production apparatus has a structure in which an anode plate / anode chamber / anion exchange membrane / anion exchange region / intermediate ion exchange membrane / cation exchange region / cation exchange membrane / cathode chamber / cathode plate are arranged in this order. The electric deionized water production apparatus according to claim 2 or 3 .

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