TWI358392B - - Google Patents

Description

1358392 IX. Description of the Invention: [Technical Field of the Invention] The present invention relates to various industrial aspects such as a semiconductor manufacturing industry, a pharmaceutical industry, a food industry, a power generation institute, a research institute, etc. using deionized water, or syrup, juice, and wine. The electric-type deionized water production device used for manufacturing, etc. [Prior Art]

In the method of producing deionized water, a method of performing deionization by treated water in a granular ion exchange resin (hereinafter referred to as "ion exchange resin") has been known, and in this method, if an ion is used When the ion exchange capacity of the exchange resin is lowered, it is necessary to carry out regeneration treatment by using a chemical. In order to eliminate the disadvantage of such a treatment operation, it is possible to establish a deionization method by an electric deionization method which does not require regeneration by a chemical at all. The water production method has reached the practical stage. The above-mentioned conventional deionized water production apparatus basically consists of a mixed ion exchange between an anion exchange resin used as an ion exchanger and a cation exchange resin in a gap formed by a cation exchange membrane and an anion exchange membrane. The resin layer forms a deionization chamber, passes the water to be treated through the ion exchange resin layer, and flows the water to be treated through the two ion exchange membranes, and applies a direct current in a vertical direction to oxidize ions in the water to be treated. The electric discharge is made of deionized water while being concentrated in water flowing outside the two ion exchange membrane. On the other hand, in Japanese Patent Laid-Open Publication No. H03- 3 3 4 5 60, it is disclosed that a monolithic organic porous ion exchanger is filled (hereinafter referred to as 312XP/invention specification (supplement)/ 94-11/94124854 6 5

1358392 "Separate block j" deionization chamber, water is discharged from the deionization chamber, and ionic impurities are removed, helium is produced, and a DC electric field is applied to the desorption chamber. The ionic impurities on the mass ion exchanger are excluded from the electrical deionized water outside the system, and the DC electric field is applied in the opposite direction according to the water passing direction of the excluded ions in the organic ion exchange body. An electric deionized water production apparatus for performing a swimming movement. The ion chamber of the electric deionized water production apparatus described in Japanese Patent Laid-Open Publication No. 2003-334560 has a large width dimension and a three-dimensional network is used for the deionization chamber filler. The monolith of the structure is therefore simpler than the direct current flow applied to the previous electrical deionized water applied in the vertical direction, and the material cost and the processing fee are also reduced. Because the monolith is in a continuum state compared to the underlying layer of the granular ion exchange resin, the adsorption/desorption of ions is more soluble in the adsorbed ionic impurities. The movement is relatively fast, and the adsorption can be easily eliminated, and the effect of scaling such as calcium carbonate or magnesium hydroxide does not occur at all. (Patent Document 1) Japanese Patent Laid-Open No. 2 0 0 3 - 3 3 4 5 In the deionized water production apparatus described in Japanese Laid-Open Patent Publication No. H03- 3 3 4 5 60, the ion exchange capacity is small only when the single separator is filled in the deionization chamber. The water quality of the treated water is weaker. Moreover, as with the granular ion exchange resin, if only a single exchange body is filled in the container, the expansion and contraction due to the ion exchange reaction will occur, resulting in a filling state. The problem of change. 312XP / invention manual (supplement) / 94-1 丨 / 94〗 24854 Water ion adsorption to build a porous device to open the water device, group, easy to 'Ion can be electrical, because 75 1358392, the ion exchange resin is used as an example to illustrate the expansion and contraction mechanism of the filler in the container. The expansion ratio is, for example, cation exchange resin 7% and anion exchange resin 23%. When the ion exchange resin refers to the transition from a state of a salt form of reproduction, the varying volume ratio. For example, in a volume of 160 mm, a tank is filled with 160 ml of an anion exchange resin in a regenerated form (R-OH), and the water to be treated is passed through water for a certain period of time, when the R-OH of the anion exchange resin is completely converted into R-Cl, In the case of salt forms such as RN〇3 and R-HC〇3, 160 ml of anion exchange resin will reduce the volume by about 30%, as calculated by 1 60 m 1 +1 . 2 3 = 1 3 0 . 1 m 1 Less β. With this phenomenon, only the water phase portion of the unfilled resin appears in the deionization chamber, and the water overflow (s h e d ) condition occurs, and the voltage rises remarkably, so that the current necessary for ion removal cannot be circulated. On the contrary, when the volume is 160 ml, filled with an anion exchange resin of 160-m m 1 in the form of a salt such as R-Cl, RN〇3, R-HC〇3, etc., and subjected to electrical regeneration for a certain period of time. The anion exchange resin will be completely converted to R - Ο Η, and the anion exchange resin of 1600 m 1 will be calculated as 1 60 m 1 X 1. 2 3 = 1 9 6 . 8 m 1 , ion exchange resin The volume should be increased. However, in this case, since there are containers constituting the deionization chamber,

Therefore, the stress will be concentrated in the portion where the strength of the sub-chamber is the lowest, causing damage and a problem of increased water flow resistance. Monoliths also have the properties of expansion and contraction like ion exchange resins, and the volume will vary to the same extent. In order to solve the problem of expansion and contraction of such a single ion exchanger, the volume ratio of the salt form to the regenerated form of the ion exchanger to be filled in the deionization chamber is determined in advance, but the electric deionized water production device is used. In the continuous operation, the water quality and current efficiency of the water to be treated are determined, and the ratio of the salt form or the regenerative form in the sub-chamber is determined. 5 3 UXP/Invention Manual (Supplement V94·II/94!24854 1358392) It is not possible to pre-determine a certain volume and then fill it. In this case, it is eager to develop an electric type that can be maintained by the patent publication No. 2 0 0 3 - 3 3 4 5 6 0 The ionized water producing apparatus has an advantage of being able to solve the problem of an electrical deionized water producing apparatus which overflows due to expansion or contraction caused by the ion exchange reaction and which has a problem of poor contact with the ion exchange membrane.

Therefore, the object of the present invention is to provide a device having a simple structure and reducing material cost, processing cost and assembly cost, and the adsorbed ionic impurities move rapidly, and the adsorbed ions can be easily removed without being expanded by the ion exchange reaction. An electric deionized water production apparatus that shrinks and causes an overflow condition or a contact failure with an ion exchange membrane. SUMMARY OF THE INVENTION In view of the above circumstances, the inventors of the present invention have been able to solve the above problems of the conventional electric deionized water producing apparatus, and have found through intensive research that the ion exchanger filled in the deionization chamber is a single The mixture of the block and the ion exchange resin can prevent the expansion and contraction caused by the ion exchange reaction by the buffering effect caused by the physical expansion and contraction of the expansion and contraction derived from the ion exchange reaction derived from the monolith. Since the overflow or the contact with the ion exchange membrane occurs, a wide deionization chamber structure that cannot be achieved by a single ion exchanger can be used, and the structure is simple, and the material cost, processing fee, assembly cost, etc. can be reduced. invention. In other words, the electric deionized water production apparatus according to the invention (1) is in the same direction as the water passing direction of the excluded ions in the deionization chamber filled with the ion exchanger. Or the opposite direction into the 312XP / invention manual (supplement) /94-11 /94124854 9 5 1358392 line to move the application of a direct current electric field, the ionic impurities absorbed on the ion exchanger, excluded from the electrical system outside the system The deionized water production device; wherein the ion exchange system is a mixture of monolithic organic porous ion exchange and granular ion exchange resin. Further, the electric deionized water production apparatus according to the invention (2) includes: a deanionization chamber, an anion tank, a decationization chamber, and a positive subtank; and the deanionization chamber is provided by one side anion exchange membrane Separating from the other side sub-exchange membrane; the anion tank has an anode disposed outside the side of the β-sub-exchange membrane, and a cathode disposed on the side of the other side of the ion exchange membrane, and One side of the anion chamber is adjacent to the anion exchange membrane, and the treated water is supplied, and from the other side of the deionization chamber, the first treatment water is obtained near the membrane; the decationization chamber is made up of one side of the anode The exchange membrane is separated from the other side of the ion exchange membrane; the cation tank is: a cathode disposed outside the cation exchange membrane on the one side, and an anode disposed outside the ion exchange membrane on the other side, and from the cation The first water of the anion tank is supplied in the vicinity of the I-side cation exchange membrane in the chamber, and the second treated water is obtained from the vicinity of the other ion exchange membrane in the decationization chamber. Further, the electric deionized water production apparatus according to the invention (3) includes: a decationization chamber, a cation tank, a deanion chamber, and an ion tank; and the decationization chamber is exchanged by one side cation The membrane is separated from another ion exchange membrane; the cation tank has a cathode disposed outside the ion exchange membrane on the one side, and an anode disposed outside the ion exchange on the other side, and from the decationization chamber One side of the cation exchange membrane attachment body is attached to the externally attached and attached to the side of the yin side of the yin membrane 312 ΧΡ / invention manual (supplement) / 94- ] 1 / 94124854 10 5 1358392 Treating water and obtaining first treated water from the vicinity of the other ion exchange membrane in the decationization chamber; the deanion chamber is separated from the other ion exchange membrane by one side anion exchange membrane; the anion tank And an anode disposed outside the anion exchange membrane on the one side, and a cathode disposed outside the ion exchange membrane on the other side, and from the vicinity of the anion exchange membrane on one side of the deanionization chamber, The first treated water of the cation tank is supplied, and the second treated water is obtained from the vicinity of the other ion exchange membrane in the deionizing chamber.

Further, in the above-described electric deionized water production apparatus according to the invention, the ion exchange body filled in the cathode side of the cation tank is a monolithic organic porous cation exchanger or an anode. An ion exchange system monolithic organic porous anion exchanger filled in the side; an ion exchange system monolithic organic porous anion exchanger filled in the anode side of the anion tank, or an ion filled in the cathode side Exchange system monolithic organic porous cation exchanger. Further, the above-described electric deionized water producing apparatus according to the invention (5) is characterized in that an intermediate ion exchange membrane is provided between the one side anion exchange membrane and the other side cation exchange membrane, and an anion is formed from the one side. a deionization chamber separated from the intermediate ion exchange membrane; and a decationization chamber partitioned by the other side cation exchange membrane and the intermediate ion exchange membrane, and outside the anion exchange membrane on the side Arranging an anode, disposing a deionization tank of the cathode outside the cation exchange membrane on the other side; wherein, from the vicinity of the cation exchange membrane in the other side of the decationization chamber, treated water is supplied from the decationization chamber In the vicinity of the intermediate ion exchange membrane, water of the first treatment 312XP/invention specification (supplement)/94-11/94124854 11 5 1358392 is obtained, and the first treatment is supplied from the vicinity of one of the anion exchange membranes in the deionization chamber. Water, and the second treated water is obtained from the vicinity of the intermediate ion exchange membrane in the deanionization chamber.

Further, in the above-described electric deionized water producing apparatus according to the invention (6), an intermediate ion exchange membrane is provided between the one side cation exchange membrane and the other side anion exchange membrane, and the one side cation is formed a deionization chamber separated from the intermediate ion exchange membrane; and a deanionization chamber separated from the intermediate exchange membrane and the intermediate ion exchange membrane, and outside the cation exchange membrane on the side a cathode is disposed, and an anode deionization tank is disposed outside the anion exchange membrane on the other side; wherein the treated water is supplied from the vicinity of the anion exchange membrane in the other side of the deanionization chamber, and is discharged from the deionization chamber The first treated water is obtained in the vicinity of the intermediate ion exchange membrane, and the first treated water is supplied from the vicinity of one of the cation exchange membranes in the decationizing chamber, and is in the vicinity of the intermediate ion exchange membrane in the decationizing chamber. The second treated water was obtained. Further, in the above-described electric deionized water production apparatus according to the invention (7), the ion exchange body filled in the cathode side of the decationization chamber is a monolithic organic porous cation exchanger, or the above-mentioned The ion exchanger filled in the anode side of the anion chamber is a monolithic organic porous anion exchanger. Further, the electric deionized water production apparatus according to the invention (8) is provided with a deionization chamber partitioned by one side anion exchange membrane from the other side cation exchange membrane, and disposed on the side An anode outside the anion exchange membrane, and a cathode disposed outside the cation exchange membrane of the other side; and the anode side of the deionization chamber is filled with a single sheet at 312XP/Invention Manual (Supplement)/94-11/94124854 12 5 1358392 a bulk organic porous anion exchanger; or a deionization tank in which a monolithic organic porous cation exchanger is filled on the cathode side of the deionization chamber: from the vicinity of the anion exchange membrane in one of the deionization chambers Supplying treated water, obtaining treated water from the vicinity of the other side of the cation exchange membrane in the deionization chamber, or supplying treated water from the vicinity of the other side of the cation exchange membrane in the deionization chamber, and Treated water is obtained from the vicinity of one of the anion exchange membranes in the deionization chamber. According to the present invention, since a part of the ion exchange® body to be filled in the deionization chamber is a single block, the volume change due to the expansion and contraction reaction of the monolith and the ion exchange resin will be available. The physical flexibility of the block is buffered, and the filling state in the deionization chamber can be maintained in a uniform state. In addition, since it is possible to prevent the occurrence of overflow and the poor contact with the ion exchange membrane due to the ion exchange reaction, the expansion and contraction conditions are formed, so that a wide space and simplification which cannot be achieved by forming a single ion exchange resin can be achieved. Deviation from the sub-exchange chamber structure can reduce material costs, processing costs and assembly costs. In addition, compared to the ion exchange resin, 9 ' because the monolithic ions move faster, and the length of the ion exchanger is shorter, the monoliths disposed near the inlet of the treated water will promote ion emission. The treatment of high ion concentration water can be performed, and the monolith disposed near the treatment water outlet can suppress the occurrence of trace ion leakage in the lean concentration region to obtain high purity treated water. In addition, by arranging a monolith in the vicinity of the treated water inlet of the deionization chamber, the removal rate of the hardness component such as calcium in the decationization chamber is increased, and the anion such as carbonic acid and cerium oxide in the deionization chamber is raised. Exclude speed. In addition, compared to the single 5 312XP / invention specification (supplement) / 94-11/94124854 1358392 block phase, because the water exchange resistance of the ion exchange resin phase is very small, the ions arranged near the inlet of the treated water stream By exchanging the resin phase, it has the function of forming a distribution pipe that flows equally in the deionization chamber, and it is possible to prevent the overflow from occurring in the deionization chamber. Further, if the ion exchange resin phase is further disposed near the treatment water outlet, the occurrence of the overflow condition can be further prevented. [Embodiment] The basic structure of the electric deionized water production apparatus of the present invention is a mixture of a monolith and an ion exchange resin filled in a deionization chamber partitioned by a Φ two-side ion exchange membrane. Deviating from the sub-chamber, and arranging an electrode for applying a DC electric field outside the ion exchange membrane, the DC electric field is applied in the same or opposite direction to the excluded water in the direction of water passing through the ion exchange body Apply by way of swimming. The "moving in the same or opposite direction" also covers the movement in the same direction as the opposite direction. In the present invention, the "water-passing direction in the mixed ion exchange body" means the water-passing direction at the approximate central portion of the mixed ion exchange body. For example, as shown in Fig. 2, the treated water inlet and the treated water outlet are on the side view, located on a slightly diagonal line, and the flow in the mixed ion exchange body is not in a single direction (in other words, the left and right direction in the figure), but actually Most of the water in the mixed ion exchange body is oriented in the left and right direction, and such water passing form is also encompassed by the present invention. Further, in the mixed ion exchange body, it is not necessary to separately provide the water to be treated introduction portion and the treated water collection portion, but it may be provided even if it is installed. The monolithic organic porous ion exchanger is not particularly limited, and is disclosed in, for example, 曰145 312XP/Invention Manual (Supplement)/94-11/94124854 1358392 Patent Open 2 Ο Ο 3 - 3 3 4 5 6 0 The substances described can be used in the interconnected macropores and macroporous walls, and have an open-cell structure with pores with an average diameter of 1 - 1 0 0 0 ^ m. The total pore volume is from 1 ml/g to 50 ml/g. The ion exchange group is uniformly distributed, and the ion exchange capacity is 55 mg equivalent/g of the three-dimensional network structure above the dried porous body. The granular ion exchange resin is not particularly limited, and is, for example, a known ion exchange resin used in water treatment. The mixture of the monolith and the ion exchange resin is not particularly limited, and is, for example, a layered body in which a monolithic phase and an ion exchange resin phase are laminated in a direction of water flow (direction in which ions are ejected). The monolithic layer and the ion exchange resin layered body, since the monolithic structure is a spongy one-piece structure, it will not be mixed with the ion-exchange resin, and even if an ion exchange membrane or the like is not used in the container, Can still be filled into a phase. The volume ratio of the monolayer phase of the layered body to the ion exchange resin phase is not particularly limited, and can be appropriately determined depending on the type of the ion exchange group, the purpose of treatment of the water to be treated, and the like. Further, the layer I structure of the layered body is not particularly limited, and for example, from one ion exchange membrane to the other side, an ion exchange membrane is sequentially formed, and a monolith phase, an ion exchange resin phase, and an ion exchange resin phase are sequentially formed. a two-layer structure with a monolithic phase; or a three-layer structure of a monolithic phase, an ion exchange resin phase and a monolithic phase, an ion exchange resin phase, a monolithic phase, and an ion exchange resin phase; or a repeating monolithic phase and ion exchange A four-layer structure of a resin phase, and the like. In the case where a monolithic phase is disposed in the vicinity of the inlet of the treated water, the removal rate of the hardness component such as calcium ions in the decationization chamber is increased, and the anion such as carbonic acid and cerium oxide in the deionization chamber is raised. The speed of elimination. In addition, if it belongs to the treatment in the deionization chamber 312XP / invention manual (supplement) /94-11 /94124854 15 5 1358392 water flow removal, the exit, the fat phase, the tree replacement function

Ions can only be mixed by the slowdown k

2cm) The interelectrode electrode continues to be regenerated and the sub-single block has a form of a cation monoblock in the vicinity of the R-Na outlet, so that a small amount of cations that cannot be removed in the cation chamber can be surely removed. Further, if it is in the vicinity of the inlet of the water, or in the vicinity of the inlet of the treated water and the vicinity of the treated water, the ion exchange resin is disposed, because the ion exchange tree has a very small water flow resistance compared to the monolithic phase. The ion-to-lipid phase has a distribution tube that forms an equal flow in the deionization chamber, thereby preventing an overflow condition in the deionization chamber. The mixed ion form of the block and the ion exchange resin is not particularly limited, but it is preferably a mixture of a salt form and a regenerated form, which can alleviate the expansion and contraction caused by the exchange reaction. Further, in the present invention, the expansion and collection effect by the mixture of the monolith and the ion exchange resin is not sufficient, but if the physical expansion and contraction effect of the monolith is added, the adhesion in the sub-chamber is ensured. The expansion and contraction of the relevant monolith and the ion exchange resin body will be described by taking a cation tank as an example. Fig. 1 (A) The ion channel is from the cathode side toward the anode side, and is sequentially filled with: R - N a ion exchange resin 40 ml (section 4x5 = 20cm2, electrode length, R - Η granular cation exchange resin 80) m 1 (戠4 X 5 = 2 0 c m2, electrical length 4 cm), and R-Na cation monolith 40 ml (load surface 4x5 = 20 cm2, length 2 cm). When continuous water flow is applied to the above cation tank In the case of continuous growth, usually the R-Na granular cation exchange resin will partially re-expand, and the R-N-granular cation exchange resin will not change, and the R-N a cation will regenerate and expand. At this time, from R - The cation in which R is regenerated to R-Η will swell, but it will disintegrate into a sponge-like shape (concave shape), and absorb the expansion of the granular cation exchange resin, so the density of each ion exchanger is (S) 312XP/Invention Manual (Supplement) /94-11 /94124854 16 1358392 The joint will be lifted and will be well-balanced in the container (Fig. 1(B)). On the other hand, continuous water/continuous regeneration is carried out for the above cation tank. At the same time, the ion load of the treated water is higher, and the ion accumulation tendency is more balanced than the initial filling state. In the case of the ion exchanger, the continuous treatment is carried out in a state in which the length of the ion exchanger extends from the inlet side (cathode, ion exclusion side) to the treated water outlet (anode, regeneration side). In this case, R - N a The cation exchange resin does not change, part of the RH granular cation exchange resin will change to the salt form and shrink, and the R-Na cation monolith will regenerate into RH and expand. At this time, since it is regenerated from R-Na to RH The cationic monolith will fill the volume-reduced fraction of the R-Η granular cation exchange resin, and thus, as described above, the adhesion of each ion exchanger will be improved, and the well-balanced container is accommodated in the container (Fig. 1 (C) In the present example, the R-N a granular cation exchange tree is described as an example in which the fat and the R - Η granular cation exchange resin are filled in a layered form, but it is not limited thereto, and may be used in combination. The situation will also be as good as the above.

In the present invention, the water to be treated is intended to be deionized, and only the turbid substance is not contained, and the rest is not particularly limited, and is, for example, industrial water or tap water having a turbidity of about 1 degree or less. Next, an electric deionized water producing apparatus according to a first embodiment of the present invention will be described with reference to Fig. 2 . Fig. 2 is a schematic view showing the construction of the electric deionized water producing apparatus of this embodiment. The electric deionized water production apparatus 2 of Fig. 2 is composed of an anion tank 20a which mainly removes anionic impurities from the water to be treated, and a cation tank 20b which mainly removes cationic impurities from the treated water of the anion tank 20a. Composition. 312XP/Invention Manual (Supplement)/94-11/94124854 17 5 1358392 Anion tank 2 0 a is in a deionization chamber separated from one side of the anion exchange membrane 2 and the other side of the cation exchange membrane 1 The side of the anion exchange membrane 2 is sequentially filled with the anion monolith 14 and the anion exchange resin 11, and constitutes the deanion chamber 7, and the anode 10 is disposed on the outer side of the one anion exchange membrane 2, and the cation is on the other side. The cathode 9 is disposed outside the exchange membrane 1, and the treated water is supplied from the inlet 3a near the anion exchange membrane 2 on one side (anode side) of the deanion chamber 7, and is supplied from the other side of the deanion chamber 7 (Cathode side) The outflow port 4a in the vicinity of the cation exchange membrane 1 was obtained as the first point β water. In other words, the water-passing direction in the deionizing chamber 7 of the anion tank 20a is in the direction from left to right as indicated by the direction of the solid arrow in Fig. 2 . The filling ratio of the anion monolith 14 and the anion exchange resin 1 1 can be arbitrarily determined depending on the physical properties of the water to be treated, and the like: preferably, the volume ratio of the ion exchange resin is 1:0.5 to 1:10.

On the other hand, the cation tank 20b is in a deionization chamber partitioned by the one side cation exchange membrane 1 and the other side cation exchange membrane 1, and is sequentially filled with a cationic single from one cation exchange membrane 1. The block 13 and the cation exchange resin 12 constitute the decation chamber 6, and the cathode 9 is disposed outside the one side cation exchange membrane 1, and the anode 10 is disposed outside the other side of the cation exchange membrane 1, and The inlet 3b in the vicinity of the cation exchange membrane 1 on one side (cathode side) of the cation chamber 6 is supplied with treated water (first treated water) of the anion tank 20a, and from the other side of the decationizing chamber 6 (anode side) The outlet 4b in the vicinity of the cation exchange membrane 1 is obtained as treated water (second treated water). In other words, the water passing direction in the cation chamber 6 of the cation tank 20b is a left-to-right direction as indicated by the direction of the solid arrow in Fig. 1. The cationic monolith 13 312XP / invention specification (supplement) / 94-1 丨 / 94] 24854 18 5 1358392 The filling ratio of the cation exchange resin 12 can be arbitrarily determined depending on the physical properties of the water to be treated, etc., preferably Block: The volume ratio of the ion exchange resin is 1:0·5~1 : 1 0 阴离子 The anion monolith 14 filled in the deanion chamber 7 of the anion tank 20a in this example, and the decation chamber 6 in the cation tank 20b The cation monolith 13 filled in the above is preferably the above monolithic organic porous ion exchanger. In addition, the shape of the decationization chamber 6 and the deionization chamber 7 is only required to move in the opposite direction to the water passing direction of the mixed ion exchange body according to the excluded ions, and the electric field can be applied, and the rest can be used. There is no particular limitation, and it is preferably in the form of a column or a cube in terms of the ease of manufacture of the members. In addition, the moving distance of the treated water, that is, the effective thickness of the mixed ion exchange filling layer of the deionization chamber 6 and the deanionization chamber 7 is set to 20 to 600 mm, preferably 30 to 300 mm, which will contribute to When the resistance 値 and the water-passing differential pressure are suppressed, the deionization process is surely performed.

The cation exchange membrane, the anion exchange membrane, the cathode, the anode, the arrangement of the electrode and the ion exchange membrane, the DC current arrangement, and the DC current electrification method are as described in Japanese Patent Laid-Open No. 2000- 3 3 4 5 6 0 Recorded in the middle. Further, in the anion tank 20 a, a non-conductor spacer 8 such as a polyolefin mesh is interposed between the anode and the anion exchange membrane in order to avoid direct contact between the anode and the anion exchange membrane. Thereby, it is possible to prevent the deterioration of the anion exchange membrane from occurring due to the strong oxidation on the anode side. In the anion tank 20 a and the cation tank 20 b, the treated water flows into the mixed ion exchange body, and the collected from the mixed ion exchange body 5 312XP / invention specification (supplement) / 94-11 / 94124854 19 1358392 The method of water management is not particularly limited, and it is only necessary to flow into the treated water or the treated water from the inflow port or the outflow port provided in the vicinity of the ion exchange membrane filled with the container in which the ion exchanger is mixed. can. Further, for example, a distribution pipe and a water collecting pipe in which pores are formed in the pipe may be formed in a concentric shape by forming a flow of the equal water to be treated in a deionization chamber and fitting the shape of the deionization chamber. Or a method of equally spaced parallel lines, or cutting a groove in a single treated water collecting part or a first treated water introducing and distributing part, so that the single piece itself has a treated water collecting function or is treated with water The method of distributing functions, etc. Further, the method of operating the electric deionized water production apparatus 20A of the present embodiment may be either continuous operation or intermittent operation, for example, depending on the continuous flow of water and continuous energization of the treated water to the apparatus. The method, ^, and the intermittent operation method of stopping the flow of the water to be treated for a certain period of time and performing the direct current only during the water stop time. In the anion tank 20a, the water to be treated is introduced from the inlet 3a near the anion exchange membrane 2 on the anode 10 side of the deanion chamber 7. Then, treated water

In the anion monolith 14 and the anion exchange resin 11, the anion Y- is adsorbed and removed, and moves toward the cathode 9 to form first treated water, and is in the vicinity of the cation exchange membrane 1 from the cathode 9 side of the deanion chamber 7. The outflow port 4a is discharged. Then, the first treated water is introduced into the vicinity of the cathode 9 and the side cation exchange membrane 1 in the decationization chamber 6 of the cation tank 20b through the communication tube 5a and the inlet 3b. Then, the first treated water of the water to be treated moves in the cation monolith 1 and the cation exchange resin 1 2 while adsorbing and removing the cation enthalpy, and moves toward the anode 10 side to form the second portion 2. 5 312XP/Invention Manual (supplement)/94-11/94丨24854 1358392 Water is drained from the outlet port 4b near the cation exchange membrane 1 on the anode 10 side of the decationization chamber 6.

The anion cesium adsorbed by the anion monolith 14 and the anion exchange resin 11 in the deanionization chamber 7 is electrically connected by the applied direct current between the cathode 9 and the anode 10 disposed at both ends of the deanionization chamber 7. In the case of the migration, the anion sputum will pass through the anion exchange membrane 2 on the anode 10 side and be discharged as an anode chamber (not shown). Similarly, the cation X+ adsorbed by the cation monolith 13 and the cation exchange resin 12 in the decationization chamber 6 is applied between the cathode 9 and the anode 10 disposed at both ends of the decationization chamber 6. The direct current is electrically flowed and discharged to the cathode chamber (not shown) through the cation exchange membrane 1 on the cathode 9 side. The impurity anions discharged into the anode chamber are taken up by the electrode water flowing in from the inlet of the anode chamber and flowing out of the anode chamber outlet, and are discharged outside the system. Similarly, the impurity cations discharged into the cathode chamber will be taken up by the electrode water flowing in from the cathode chamber inlet and out of the cathode chamber outlet, and discharged out of the system. The electrode water may also partially flow the treated water into the four electrode chambers independently, or may form a state in which the two systems flow in the anode water system and the cathode water system, respectively. In addition, the electrode water can flow frequently, and can also be appropriately intermittently flowed. This method is because an anionic monolithic phase is disposed in the anion tank 20 a near the inlet of the treated water to enhance the elimination rate of anions such as carbonic acid and cerium oxide, and thus, for example, a permeated water of a reverse osmosis membrane, It is particularly effective when the water contains more free carbonic acid. According to this device, because the 215 312XP/invention manual (supplement) /94-11 /94124854 1358392 mixes the monolith and ion exchange resin into a layer in the tank, it will make up for the ion exchange capacity caused by the use of a single block. Reduce the situation. Further, the volume change due to the expansion and contraction reaction of the monolith and the ion exchange resin is moderated by the physical stretchability of the monolith, and the state of filling in the deionization chamber can be uniformly maintained. In addition, since the impurity cations and the impurity anions will be discharged out of the apparatus, respectively, the mixing condition will not occur in the apparatus as in the conventional electric deionized water production apparatus, even if the treated water contains hardness components such as calcium and magnesium. In the case of the situation, there is still no scaling in the beta. Further, in the water-passing method of the electric-type deionized water producing apparatus 20, in addition to the above method, for example, the treated water may be treated by the cation tank 20 b -, and then the treated water of the cation tank 20b may be treated with an anion. A method of performing processing in the slot 20a t. According to this method, since the calcium ions and the magnesium ions are removed by the passage of the cation tank at the beginning, the occurrence of fouling in the anion tank 20a can be prevented, and since it is in the cation tank 20b near the inlet of the treated water stream The cationic monolithic phase is disposed, thereby increasing the elimination rate of calcium ions and magnesium ions. Therefore, this method is an effective method for treating treated water containing hardness components such as calcium and magnesium. In the electric deionized water production apparatus 20A of the present embodiment, the mixed ion exchanger filled in the deanionization chamber 7 has, in addition to the above-described form, a cation from the one side (anode side) to the other side. The exchange membrane 1 > is sequentially filled with an anion exchange resin and a cation monoblock, or filled with an anion monoblock, an anion exchange resin, and a cation monoblock. The ion exchange membrane on the cathode side is determined to be a cation exchange membrane or an anion exchange membrane depending on the ion exchanger filled in the vicinity, and 312XP/invention specification (supplement)/94-11 /94124854 22 5 1358392. When the anion exchange resin and the cationic monolith are filled, the filling state of the deionizing chamber can be maintained in a uniform state by buffering the physical flexibility of the cationic monolith, and even a simple polishing function can be obtained. And because the inflow port 3a is located in the anion exchange resin phase, it is possible to prevent an overflow condition from occurring in the deionization chamber. In addition, when an anion monolith, an anion exchange resin, and a cationic monoblock are sequentially packed, the above carbonic acid and the second

The removal rate of the impurity anion such as cerium oxide has a simple polishing function, and the physical expansion of the two monoliths can uniformly maintain the filling state in the deionized ion chamber. Further, in the same manner as the mixed ion exchanger filled in the decationizing chamber 6, an appropriate ion exchanger can be selected. Similarly, in the same manner, the treated water may be treated in the cation tank 20b, and then the treated water of the cation tank 20b may be treated in the anion tank 20a. Next, an electric deionized water producing apparatus according to a second embodiment of the present invention will be described with reference to Fig. 3 . Fig. 3 is a schematic view showing the construction of the electric deionized water producing apparatus of this embodiment. In Fig. 3, the same components as those in Fig. 2 are denoted by the same reference numerals, and the description thereof will be omitted, and only the different portions will be mainly described. The electric deionized water producing apparatus 20B shown in Fig. 3 differs from Fig. 2 in that one set of electrodes is omitted, and a deionization ion chamber and a deanion chamber are provided between the one set of electrodes. In other words, in the electric deionized water producing apparatus 20B of this example, the intermediate cation exchange membrane 1 is disposed between the one side cation exchange membrane 1 and the other side anion exchange membrane 2, and the cation exchange membrane 1 is provided on one side. The intermediate cation exchange membrane] is separated from the first] deionization chamber 312XP / invention manual (supplement) / 94 -〗 1 / 94324854 23 5 1358392

The cationic monolith 13 and the cation exchange resin 12 are filled to form the decation chamber 6, and in the second deionization chamber partitioned by the other anion exchange membrane 2 and the intermediate cation exchange membrane 1, The intermediate cation exchange membrane 1 is filled with an anion exchange resin 11 and an anion monolith 14 to form a deanionization chamber 7, and a cathode 9 is disposed outside the one side cation exchange membrane 1, and an anode is disposed outside the other anion exchange membrane 2. 10, from the other side (anode side) of the deanion 7 chamber, the inflow port 3a near the anion exchange membrane 2 supplies the water to be treated, and flows from the deanion chamber 7 to the vicinity of the cation exchange membrane 1 At the outlet 4a, the first treated water is obtained, and the first treated water is supplied from the inlet 3b near the cation exchange membrane 1 on one side (cathode side) of the decationizing chamber 6, and the intermediate cation exchange is performed from the decationizing chamber 6. The second treatment water is obtained from the outflow port 4b in the vicinity of the membrane 1. In the electric deionized water producing apparatus 20B, the water to be treated which flows in from the vicinity of the anode 10 side of the anode 10 side of the deanion chamber 7 is adsorbed and removed in the anion monolith 14 and the anion exchange resin 11. Y_ moves toward the intermediate cation exchange membrane 1 side, and then flows out from the vicinity of the intermediate cation exchange membrane 1 of the deanionization chamber 7 to be discharged as the first treated water. Then, the first treated water facilitating communication tube 5b is introduced into the deionization chamber 6 from the vicinity of the cathode 9 side cation exchange membrane 1 in the deionization ion chamber 6. Then, the first treated water moves toward the intermediate cation exchange membrane 1 while adsorbing and removing the cation X+ in the cation monoblock 13 and the cation exchange resin I 2, and proceeds from the decationization chamber 6 in the form of the second treated water. It is discharged near the intermediate cation exchange membrane 1. On the other hand, in the decationization chamber 6, adsorbed to the mixed cation exchanger 312XP / invention manual (supplement) / 94-11 /94 ] 24854 24 5 1358392 Sub-stream drainage of Shangyang 9 #排进头*换与» 可 可Take off

The cation enthalpy of the seven pairs is electrically discharged, and the applied direct current is electrically moved between the cathode 9 and the pole 10 disposed at the both ends of the device 20B, and passes through the cation exchange membrane 1 on the cathode side. And discharged into the cathode chamber (not shown). Similarly, the negative ion Y _ adsorbed by the mixed anion exchanger in the deanionization chamber 7 is similarly electrically flowed by the direct current applied between the cathode 9 and the anode 10, and is exchanged by the anion at the anode 10 side. The membrane 2 is placed in an anode chamber (not shown). In other words, the direction of the passage in the deanion chamber 7 is from the right-to-left direction indicated by the direction of the solid arrow in FIG. 3, and the anion removed is swung in the opposite direction to the water-passing direction of the mixed ion exchange body. The water passing direction in the decationizing chamber 6 is from left to right in the direction of the solid arrow, and the excluded cations will migrate in the opposite direction of the water passing direction of the mixed ion body. The filling ratio of the monolith and the ion exchange resin in the deionizing chamber 7 in the decationizing chamber 6 is arbitrarily determined depending on the physical properties of the treated water, etc., preferably, the monolithic: ion exchange resin has a volume ratio of 1:0.5. 1 : 1 0. In addition to the same effects as the electric-type ionized water production apparatus 20A of the first embodiment, the electric-type ionized water production apparatus 20B according to the second embodiment can be omitted by omitting one set of poles. Miniaturization and simplification. Further, in the water-passing method of the electric deionized water producing apparatus 20B, in addition to the above method, for example, the treated water may be treated in the decationizing chamber 6, and then the treated water of the decationizing chamber 6 is deionized. The method of processing in the room. According to this method, since the calcium ions and the magnesium ions are removed by the water passing through the decationizing chamber 6 from the beginning, the fouling condition in the deanionizing chamber 7 can be prevented, and since the degassing 312XP/invention specification (Supplement) /94-11/94124854 25 5 1358392 In the ion chamber 6, a cation monolith phase is disposed in the vicinity of the inlet of the treated water, and thus the removal rate of calcium ions and magnesium ions is increased. Therefore, it is an effective method for treating treated water containing hardness components such as calcium and magnesium. In the electric deionized water production apparatus 20B of the present embodiment, the mixed ion exchanger filled in the decationization chamber 6 has, in addition to the above-described form, a cation exchange membrane 1 from one side (cathode side) toward the intermediate ion. The exchange membrane 1 is filled with a form of a cation exchange resin and an anion monolith, and is filled with a cation monoblock, a cation exchange resin, and an anion monoblock. The medium inter-Φ ion exchange membrane 1 is determined to be a cation exchange membrane or an anion exchange membrane depending on the ion exchanger filled in the vicinity. When filled with a cation exchange resin and an anionic monolith, it will be buffered by the physical extension of the anion monolith, and the filling state in the decationization chamber 6 can be maintained in a uniform state. It has a simple polishing function, and since the inflow port 3b is located in the anion exchange resin phase, it is possible to prevent the overflow from occurring in the deionization chamber. In addition, when the cationic monolith, the cation exchange resin, and the I anion monolith are sequentially filled, the impurity cation elimination rate represented by the hardness components such as calcium and magnesium described above can be improved, and the polishing function can be improved. The filling state in the decationizing chamber 6 is maintained in a uniform state by the physical flexibility of the two monoliths. The mixed ion exchange body filled in the deionization chamber 7 can be similarly selected as an appropriate ion exchanger. Further, in the same manner as described above, a method of treating the water to be treated in the decationizing chamber 6 and then treating the treated water of the decationizing chamber 6 in the deionizing chamber 7 can be employed. Next, an electric deionized water production 312XP/invention specification (supplement)/94-11/94124854 26 5 1358392 device according to a third embodiment of the present invention will be described with reference to Fig. 4 . Fig. 4 is a schematic view showing the construction of the electric deionized water producing apparatus of this embodiment. In FIG. 4, the same components as those in FIG. 3 are denoted by the same reference numerals, and the description thereof will be omitted, and only the different portions will be mainly described. The electric deionized water producing apparatus 20C shown in the circle 4 is different from that of Fig. 3 in that the intermediate cation exchange membrane 1 and the cation exchange resin are omitted. In other words, in the electric deionized water producing apparatus 20C of the present example, the anode 10 is disposed outside the one side anion exchange membrane 2, and the cathode 9 is disposed outside the other side of the cation exchange membrane 1, and is anion on one side. In the deionization chamber 5 in which the Φ membrane 2 is exchanged with the cation exchange membrane 1 on the other side, the anion monolith 14 and the anion exchange resin are sequentially packed from the side of the anion exchange membrane 2 on one side (anode side). 11 and the cation monolith 13 constitute a detachment from the R sub-chamber 15 and supply the treated water from the inflow port 3 c near the one side of the anion exchange membrane 2 in the deionization chamber 15, and from the deionization chamber 15 Another one

The treatment outlet water is obtained by the outflow port 4c in the vicinity of the cation exchange membrane 1 on the V side. In other words, the direction of water passing through the sub-chamber 15 is shown by the direction of the solid arrow in FIG.

The direction from left to right. In the electric deionized water production apparatus 20C, the water to be treated is introduced from the inlet 3c near the anion exchange membrane 2 on the anode 10 side of the deionization chamber 15. Then, the water to be treated moves in the anion monolith 14 and the anion exchange resin 11 while adsorbing and removing the anion Y_, and moves toward the cathode 9 side, and adsorbs and removes the cation Χ+ in the cation monolith 13 and further faces the cathode. The 9 side is moved, and then discharged as a treated water from the outflow port 4c near the cation exchange membrane of the cathode 9 side of the deionization chamber 15. In addition to the same effect of the electrical deionized water production device 27 312XP / invention specification (supplement) / 94-11/94124854 1358392 device 20B, the intermediate cationic film is omitted. The device can be miniaturized and simplified. Further, in the case of the electric deionized water producing apparatus 20C, the direction of movement of the anion plant is opposite to the direction of water passing, and the direction of movement of the cation crucible is in the same direction as the direction of passing water. Further, in the electric deionized water production apparatus 20C, the mixed ion exchanger filled in the deionization chamber 15 has, in addition to the above-described form, a cation exchange membrane from the one side anion exchange membrane 2 to the other side. 1. Sequentially filled with the morphology of the anion exchange resin 1 1 and the cationic monolith 1 3 . In this case, since the inflow port 3c is located in the anion exchange resin phase, it is possible to prevent the overflow from occurring in the deionization chamber. Further, in the above-described embodiment, the same as the other aspects, the inflow of the treated water is not limited to the above-described embodiment, and the water to be treated may flow into the inflow port near the other side of the cation exchange membrane 1 and The cation exchange body moves toward the anode 10 side while adsorbing and removing the cation X + , and then moves the I to remove the anion Y - while in the anion exchange body, and moves toward the anode 10 side, and then from the anion exchange membrane 2 The outlet of the stream obtains a method of treating the water. The filling ratio of the monolith and the ion exchange resin in the deionization chamber 15 can be arbitrarily determined depending on the physical properties of the treated water, etc., preferably, the monolithic ratio of the ion exchange resin is 1: 5 to 1 : 1 0 ° The electric deionized water production device of the invention can perform the same application and combination as the conventional ion exchange device, for example, a desoftening chamber is used to form a softening device, and a mixed bed ion exchanger is installed in the latter stage. It can further improve the purity of the treated water, etc. β 312ΧΡ/Invention Manual (supplement)/94-11/94124854 28 η

1358392 (Embodiment) The following is a more detailed description of the present invention, but is not intended to limit the invention. (Production of Electrical Deionized Water Manufacturing Apparatus) An electric type dewatering apparatus having the following specifications as shown in the schematic view of Fig. 5 was used. • Groove size: 160ml (longitudinal 5cmx horizontal 4cmx high (inter-electrode length) 8cm); • Tank container: inner volume 160ml; Φ · anion exchange resin (filled on the anode side): 1 2 0 m 1 ( IRA 4 0 2 BL ), 5cmx horizontal 4cmx high 6cm; • cation monolith: the monolith described in the Japanese Patent Laid-Open No. 2 0 0 3 - 3 3 4 5 60, cut into 5 cm in length and 4 cm in width X Height 2 cm; • Water to be treated: Reverse osmosis membrane permeate water, conductivity is about 20 // S / cm, flow is 15 liters / hour • Electrode water: anode water, cathode water are flow 5 liters / hour each ( Operation of the electric deionized water production apparatus) In the obtained electric deionized water production apparatus, the flow rate of the treated water is 15 liters/hour (LV = 7.5, SV = 9 4 (overall)). Through the water, the DC current of 0 3 3 A is energized, and the treated water of 0.8//S / cm is obtained according to the operating voltage of 6 4 V, showing that the electric type dewatering device according to the present invention can generate purity. High purity water. Further, in the continuous rotation, it was found that the anion exchange resin was expanded in the observation container, the cations were collapsed, and the mixed ion exchanger was in a state of being in close contact with the container. (Industrial Applicability) Only the sub-transformation rate is based on the sub-rate 312XP/invention specification (supplement)/94-11/94124854 29 5 1358392 The electric deionized water production apparatus of the present invention is applicable to Various industrial aspects such as semiconductor manufacturing industry, pharmaceutical industry, food industry, power generation institute, and research institute using deionized water, or manufacturing aspects such as syrup, juice, and wine. BRIEF DESCRIPTION OF THE DRAWINGS Fig. 1 (A) to (C) are explanatory diagrams of expansion and contraction of a monolith-ion exchange resin mixture. Fig. 2 is a schematic view showing the structure of an electric deionized water manufacturing apparatus according to a first embodiment of the present invention. Fig. 3 is a view showing the structure of an electric deionized water producing apparatus according to a second embodiment of the present invention. Fig. 4 is a view showing the structure of an electric deionized water producing apparatus according to a third embodiment of the present invention. r Fig. 5 is a schematic view showing an electric deionized water producing apparatus used in the embodiment.

[Description of main components] 1 cation exchange membrane 2 Anion exchange membrane 3a, 3b, 3 c Inflow σ 4 a, 4b' 4 c Outflow D 5 a, 5b Connecting tube 6 Decation chamber 7 Deanion chamber 8 Spacer 312XP/ Invention description (supplement) / 94-11/94] 24854 30 5 1358392

9 cathode 10 yang pole 11 yin ion exchange tree fat 12 yang ion exchange tree fat 13 yang ion single block 14 Yin detachment single block 1 5 deionization chamber 20A , 20B , 20C electric deionization water production device 20a anion separation tank 20b cation separation tank

312XP/Invention Manual (supplement)/94-11/94124854 31 5

Claims (1)

1358392 Announcement 10, the scope of the patent application 1. An electrical deionized water production device in the deionization chamber filled with an ion exchanger, in the same direction with respect to the water passing direction of the ion exchange body Or applying a direct current electric field in a manner of migrating in the opposite direction, and excluding the ionic impurities adsorbed on the ion exchanger from the system; characterized in that the ion exchange system monolithic organic porous ion exchanger A mixture with a granular ion exchange resin. 2. The electric deionized water production apparatus according to claim 1, wherein the anion tank has an anion tank separated by an anion exchange membrane and an ion exchange membrane on the other side. a chamber; an anode disposed outside the anion exchange membrane on the one side; and a cathode disposed outside the ion exchange membrane on the other side; and the treated water is supplied from the vicinity of the anion exchange membrane on one side of the deanionization chamber, and is supplied The first treated water is obtained in the vicinity of the other ion exchange membrane in the deanionization chamber; a cation tank having: a decationization chamber partitioned by one side cation exchange membrane from the other side ion exchange membrane; a cathode disposed outside the cation exchange membrane on the one side; and ion exchange disposed on the other side An anode on the outer side of the membrane; and a first treatment water supplied from the anion tank in the vicinity of one of the cation exchange membranes in the decationization chamber, and a second treatment is obtained from the vicinity of the other ion exchange membrane in the decationization chamber water. 3. The electric deionized water producing apparatus according to claim 1, wherein the cation tank is provided with: a cation exchange membrane on one side and the other side from the 312XP/invention specification (supplement)/ 94-11/94124854 32 5 1358392 a decationization chamber partitioned by a sub-exchange membrane; a cathode disposed outside the cation exchange membrane on the one side; and an anode disposed outside the ion exchange membrane on the other side; The treated water is supplied in the vicinity of one of the cation exchange membranes in the cation chamber, and the first treated water is obtained from the vicinity of the other ion exchange membrane in the decationizing chamber; An anion tank having: a deanion chamber separated from one side of the ion exchange membrane by one side; an anode disposed outside the anion exchange membrane on the one side; and an ion exchange membrane disposed on the other side a cathode on the outer side; and the first treated water of the cation tank is supplied from the vicinity of the anion exchange membrane in one of the deionization chambers, and the second treated water is obtained from the vicinity of the other ion exchange membrane in the deanion chamber . 4. The electric deionized water production apparatus according to claim 2, wherein the ion exchange system monolithic organic porous cation exchanger filled in the cathode side of the cation tank is on the anode side. The monolithic organic porous anion exchanger in which the ion exchange system is filled; the ion exchange system monolithic organic porous anion exchanger filled in the anode side of the anion tank, or the ion exchange filled in the cathode side System monolithic organic multi-stranded cation exchanger. 5. The electric deionized water producing apparatus according to claim 1, wherein an intermediate ion exchange membrane is disposed between one side of the anion exchange membrane and the other side of the cation exchange membrane, and an anion is formed by the one side a deionization chamber separated from the intermediate ion exchange membrane, and a decationization chamber partitioned by the other side cation exchange membrane and the intermediate ion exchange membrane, and outside the anion exchange membrane on the side Arranging the anode, the cathode deionization tank is disposed outside the cation exchange membrane on the other side 312XP / invention specification (supplement) / 94-11 / 94124854 33 8 1358392; from the other side of the decationization chamber near the cation exchange membrane Supplying treated water, obtaining first treated water from the vicinity of the intermediate ion exchange membrane in the decationizing chamber; supplying the first treated water from the vicinity of one of the anion exchange membranes in the deionizing chamber, and removing the anion from the deionized chamber The second treated water was obtained in the vicinity of the intermediate ion exchange membrane in the chamber. 6. The apparatus according to claim 1, wherein the intermediate ion exchange membrane is disposed between the one side cation exchange membrane and the other side anion exchange membrane, and the one side cation is formed. a deionization chamber partitioned between the exchange membrane and the intermediate ion exchange membrane, and a deanion compartment separated from the intermediate ion exchange membrane by the other side, and outside the cation exchange membrane on the side Disposing a cathode, disposing an anode deionization tank outside the anion exchange membrane on the other side; supplying treated water from the vicinity of the other anion exchange membrane in the deanionization chamber, and an intermediate ion exchange membrane from the deanionization chamber In the vicinity, the first treated water is obtained; the first treated water is supplied from the vicinity of one of the cation exchange membranes in the decationizing chamber, and the second treated water is obtained from the vicinity of the intermediate ion exchange membrane in the decationizing chamber. 7. The electric deionized water production apparatus according to claim 5, wherein the ion exchange system monolithic organic porous cation exchanger filled in the cathode side of the decationization chamber, or the above-mentioned An ion exchange system monolithic organic porous anion exchanger filled in the anode side of the anion chamber. 8. For example, the electric deionized water production device of the first application of the patent scope, 312XP/invention specification (supplement)/94-11/94124854 34 5 1358392 is provided with: a deionization chamber, which is provided by one side The anion exchange membrane is partitioned from the other side of the cation exchange membrane; the anode is disposed outside the anion exchange membrane; and the cathode is disposed outside the other side of the cation exchange membrane; and in the deionization chamber The anode side is filled with a monolithic organic porous anion exchanger, or in the deionization tank in which the cathode side of the deionization chamber is filled with a monolithic organic porous cation exchanger, Supplying water to be treated from the vicinity of one of the anion exchange membranes in the deionization chamber, and obtaining treated water from the vicinity of the other side of the deionization chamber; or, from the other side of the deionization chamber The treated water is supplied in the vicinity of the exchange membrane, and treated water is obtained from the vicinity of one of the anion exchange membranes in the deionization chamber. 35 (8) 312XP/Invention Manual (supplement)/94-11/94124854