JP4867720B2 - Pure water production method and apparatus - Google Patents

Description

  TECHNICAL FIELD The present invention relates to a pure water production apparatus that produces pure water by collecting city water, waste water, etc., including impurities, and more particularly, to a pure water production apparatus that supplies pure water as cooling water or process water for a fuel cell system. . Moreover, this invention relates to the pure water manufacturing method using this pure water manufacturing apparatus.

  A fuel cell power generator includes a reformer that reforms raw fuel gas such as city gas, LP gas, and methanol into a gas rich in hydrogen by steam reforming, and the reformed gas obtained by the reformer And a fuel cell main body that generates electric power using as a fuel.

  The reformed gas generated in the reformer is consumed inside the fuel cell according to the load and hydrogen utilization rate of the fuel cell, and the gas containing surplus hydrogen is led to the reformer as off-gas (fuel exhaust gas). Often configured to be burned with a burner and consumed as reforming energy.

  FIG. 5 is a basic system diagram of a water treatment device in a phosphoric acid fuel cell power generator described in the prior art section of Japanese Patent Application Laid-Open No. 2001-176535.

  The fuel cell main body 1 includes a unit cell composed of a fuel electrode 1b and an air electrode 1a sandwiching a phosphate electrolyte layer, and a cooling plate 1c having a cooling pipe disposed each time a plurality of the unit cells are stacked. Yes.

  Under the catalyst of the catalyst layer 2a, the reformer 2 separates the raw fuel such as natural gas supplied through the raw fuel supply system together with the water vapor separated through the water vapor separator 5 and supplied through the water vapor supply system. Then, it is heated by combustion heat generated by off-gas combustion in a burner and reformed into a gas rich in hydrogen to produce a reformed gas.

  The reformed gas generated by the reformer 2 is supplied to the fuel electrode 1 b of the fuel cell main body 1 via a reformed gas supply system having a CO converter 4. The off gas containing hydrogen that has not contributed to the cell reaction and flows out of the fuel electrode 1b is supplied as fuel to the burner of the reformer 2 through the off gas supply system.

  A combustion air supply blower (not shown) is connected to the burner of the reformer 2. The combustion exhaust gas from the reformer 2 is sent to a condenser 6 for water recovery, and is discharged after water recovery. The recovered water is sent to the recovered water tank 7.

  The fuel cell body 1 includes an air supply system including a blower 23 that supplies air to the air electrode 1a, and an air discharge system that supplies air containing water vapor after the battery reaction to the condenser 6 for water recovery. And are connected.

  A cooling water circulation system including a water vapor separator 5 and a cooling water circulation pump 22 is connected to the cooling pipe of the cooling plate 1 c of the fuel cell main body 1 in order to circulate cooling water when the fuel cell main body 1 generates power.

  In the steam separator 5, the two-phase flow of water and steam discharged from the cooling pipe of the fuel cell main body 1 is separated into steam and cooling water. The water vapor separated here is sent out so as to be mixed with the raw fuel going to the reformer 2. At that time, the ejector pump 3 is used to mix with the raw fuel having a low original pressure. The ejector pump 3 uses steam as a driving fluid and raw fuel as a driven fluid. The raw fuel supply system generally includes a desulfurizer (not shown).

  As described above, pure water is required for steam reforming. In addition, in a phosphoric acid type fuel cell, it is common to use pressurized water of pure water as the cooling water for the fuel cell. In this case, the cooling water has a low electrical conductivity and is a mineral system such as silica. Pure water with few foreign substances is used.

  Although a coolant other than water may be used for cooling the fuel cell, at least pure water is consumed as reforming steam in the reformer, so it is necessary to always supply pure water. For this reason, it is common that the air off-gas of the fuel cell and the water vapor in the combustion exhaust gas of the reformer are collected as condensed water by a condenser and then passed through a water purification device to be purified.

  When an ion exchange type water purifier is used as this water purifier, the water purifier is generally replaced at intervals of power generation time of about 2000 h to 3000 h when the electric conductivity is 0.5 to 1 μS / cm or more. This necessitates complicated resin replacement of the water purifier, and there is a problem that resin regeneration costs are generated.

  Therefore, in FIG. 5, an electrodeionization apparatus 10 that does not require resin replacement is adopted instead of the ion exchange type water purifier.

  The main part of the electrodeionization apparatus 10 is separated into a treatment chamber 10a and a concentration chamber 10b by an ion exchange membrane 10c, and the anion and cation of the recovered water introduced from the recovered water tank 7 through the pump 20 are separated. The ions pass through the anion exchange membrane and the cation exchange membrane, collect in the concentration chamber 10b, and are then discharged out of the system as concentrated waste water. As a result, pure water is continuously generated at the outlet side of the processing chamber 10 a and is sent to the water vapor separator 5 by the water supply pump 21.

  The treated water (pure water) is recycled to the suction side of the pump 20 for the purpose of dealing with fluctuations in the pure water supply amount while maintaining the flow rate of the treatment chamber.

  The check valve 24 provided in this circulation system supplies the recovered water in the recovered water tank 7 directly to the water vapor separator 5 via the feed water pump 21 without passing through the electrodeionization device 10. This is intended to prevent this.

  Concentrated wastewater is significantly less than about 1/3 of the water flow rate on the processing chamber side, so the concentrated chamber side system is also provided with a concentrated water circulation pump 10d in the same manner as the processing chamber side to recycle the concentrated water. In addition, while ensuring the amount of water passing through the concentrating chamber, the amount of concentrated drainage is appropriately secured.

  In FIG. 5, a mineral removing device 9 is provided on the inlet side of the electrodeionization device 10. Since the electrodeionization apparatus 10 uses an ion exchange membrane, the scaling material in the treated water introduced into the electrodeionization apparatus needs to have a low concentration. For example, the condition of silica is several ppm or less. A mineral removing device 9 is provided for removing scaling substances.

In FIG. 2 of Japanese Patent Laid-Open No. 2001-176535, an ion exchange type water purifier is provided in parallel with the electrodeionization device, and the ionization water is ionized when the quality of the deionized water from the electrodeionization device is lowered. A configuration is described in which water is passed through an exchangeable water purifier to avoid deterioration of water quality.
JP 2001-176535 A

  When the pure water is produced and supplied to the fuel cell by treating the recovered water of the fuel cell power generation device in the electrodeionization device as shown in FIG. 5 above, the fuel cell power generation is performed at the start-up of the fuel cell power generation device. There is no water discharged from the equipment, and pure water cannot be supplied. As described above, when an ion exchange type water purification device is provided in parallel with the electrodeionization device, pure water can be supplied to the fuel cell power generation device by this ion exchange type water purification device. However, in this case, since an electrodeionization device and an ion exchange type water purification device must be provided, the facility becomes large and the cost increases.

It is an object of the present invention to perform pure water production by electrodeionization and pure water production by ion exchange using an electrodeionization apparatus .

Water purifying apparatus 請 Motomeko 1, by arranging the ion exchange membrane between the anode and the cathode, provided at least the cathode compartment, the cathode-side concentrate chamber, the depletion chamber and the anode-side concentrate chamber, the cathode chamber In a pure water production apparatus having an electrodeionization apparatus in which a conductor is filled, and the cathode side concentration chamber, the desalting chamber, and the anode side concentration chamber are filled with an ion exchanger, the cathode chamber and the cathode The ion exchange membrane that divides the chamber-side concentration chamber is a bipolar membrane or a monovalent cation selective permeable cation exchange membrane. Water to be treated is passed through at least one of the concentration chambers, and ions are exchanged by the ion exchanger in the concentration chamber. An ion exchanging pure water production operation mode executing means for exchanging the pure water from the concentrating chamber is provided.

According to a second aspect of the present invention, there is provided a deionized water production apparatus according to the first aspect , wherein the ion exchange type deionized water production operation mode execution unit stops energization or includes an energization control unit that adjusts the current density to 1000 mA / dm ² or less. It is characterized by.

In the pure water production apparatus according to claim 3 , in the ion exchange type pure water production operation mode according to claim 1 or 2 , water to be treated is passed through the cathode side concentrating chamber and then the anode side concentrating. Water is passed through the room.

The pure water production apparatus according to claim 4 is the cation exchange according to any one of claims 1 to 3 , wherein an anion exchanger and a cation exchange are provided as an ion exchanger in at least one of the cathode chamber side enrichment chamber and the anode chamber side enrichment chamber. A mixed bed with a body is filled, or at least one of the cathode chamber side enrichment chamber and the anode chamber side enrichment chamber is alternately filled with a cation exchanger and an anion exchanger in this order from the upstream side. It is characterized by being.

According to a fifth aspect of the present invention, there is provided a pure production apparatus according to any one of the first to fourth aspects, wherein the conductor is a cation exchanger or a corrosion-resistant conductive metal body .

Pure water production method of 請 Motomeko 6, by arranging the ion exchange membrane between the anode and the cathode, provided at least the cathode compartment, the cathode-side concentrate chamber, the depletion chamber and the anode-side concentrate chamber, the cathode chamber In the method for producing pure water by using an electrodeionization apparatus in which a conductor is filled and an ion exchanger is filled in the cathode side concentration chamber, the desalting chamber, and the anode side concentration chamber. The ion exchange membrane that partitions the cathode chamber side concentration chamber is a bipolar membrane or a monovalent cation selective permeable cation exchange membrane, and water to be treated is passed through at least one concentration chamber, and the ion exchange in the concentration chamber is performed. An ion exchange type pure water production operation is performed in which ion exchange is performed by a body and pure water is discharged from the concentration chamber.

A pure water production method according to a seventh aspect is the method according to the sixth aspect , wherein the ion-exchange-type pure water production operation is stopped or the current supply is controlled so that the current density is 1000 mA / dm ² or less. It is characterized by being.

A pure water production method according to an eighth aspect is characterized in that, in the sixth or seventh aspect , the water to be treated is city water, well water, or water obtained by removing turbidity and dechlorination from industrial water.

The method for producing pure water according to claim 9 is the method for producing pure water according to any one of claims 6 to 8 , wherein the electrodeionization device is for purifying the recovered water of the fuel cell power generation device, and is activated when the fuel cell power generation device is started up. It is characterized in that ion-exchange-type pure water is produced by an electrodeionization apparatus, and the produced pure water is supplied to a fuel cell power generator.

According to the pure water production apparatus of claim 1 and the pure water production method of claim 6 , pure water production by ion exchange can be performed using the ion exchanger filled in the electrodeionization apparatus. Therefore, it is possible to supply pure water by ion exchange treatment without providing an electrodeionization device and an ion exchange device. In addition, since the ions that cause scale generation contained in the water to be treated are difficult to concentrate near the surface of the cathode and ion exchange resin by keeping the energization amount below the specified amount, the scale adheres to the cathode and ion exchange resin. Can be prevented.

  In this electrodeionization apparatus, a cathode chamber is provided separately from the cathode-side concentrating chamber, and both are separated by a bipolar membrane or a monovalent cation selective permeable cation exchange membrane. The movement of Ca ions and Mg ions is prevented, and the movement of anions such as hydroxide ions and bicarbonate ions from the cathode chamber to the cathode-side concentration chamber is blocked. Therefore, it is prevented that Ca ions, Mg ions, and anions are associated with each other in the cathode chamber or the cathode-side concentration chamber to generate scale.

  This bipolar membrane is a kind of composite membrane having a structure in which an anion exchange membrane and a cation exchange membrane are bonded together. Bipolar membranes have been widely used as a separation membrane for electrolysis of water or as a separation membrane for regenerating acid and alkali from an aqueous solution of a salt that is a neutralized product of acid and alkali. It is an ion exchange membrane, and various manufacturing methods have been proposed.

  Moreover, this monovalent cation selective permeable cation exchange membrane is also conventionally known, and is widely used for concentration or separation of an aqueous electrolyte solution, production of demineralized water, and the like.

This monovalent cation selective permeable cation exchange membrane is
(1) The surface portion of the cation exchange membrane has a dense structure (for example, the surface layer portion is a layer having a high degree of crosslinking or a layer having a high fixed ion concentration);
(2) forming an electrically neutral thin layer containing no ion exchange groups on the surface of the cation exchange membrane;
(3) An anion exchange thin layer (hereinafter sometimes referred to as an opposite charge layer) is formed on the surface of the cation exchange membrane:
By using these methods alone, or by using these methods together, monovalent cations are selectively permeated with almost no permeation of divalent or higher cations from the membrane surface. In the present invention, among these, it is preferable to use one that selectively permeates monovalent cations by the method (3).

  As such a monovalent cation selective permeable cation exchange membrane, for example, a thin film made of a polymer of a quaternary ammonium base and a vinyl compound having three or more vinylbenzyl groups on at least one side of the cation exchange membrane. The thing which formed the layer is mentioned. The cation exchange membrane used as the substrate is not particularly limited, and preferably has a high cation exchange selectivity. As the monovalent cation selective permeable cation exchange membrane, for example, CMS (trade name) manufactured by Astom Co., Ltd. can be used.

  In addition, by performing the ion exchange treatment operation, cations and anions such as sodium ions and chlorine ions accumulate in the ion exchanger of the electrodeionization apparatus. It is removed when the electrodeionization operation is performed, and the ion exchanger is regenerated.

Concentrated Chijimishitsu water to be treated that is passed through to the pure water production by ion exchange treatment is preferably filled from the upstream side to the alternating cation exchanger and an anion exchanger. The advantages of the alternating lamination method will be described later in detail.

< Reference example >
Hereinafter, reference examples and embodiments will be described with reference to the drawings. FIG. 1 is a schematic longitudinal sectional view of an electric deionization apparatus according to a reference example .

  Between the cathode 31 and the anode 32, a bipolar membrane 33, a first cation exchange membrane 34, an anion exchange membrane 35, and a second cation exchange membrane 34 'are arranged one by one. A cathode chamber 41 is formed between the membrane 33, a cathode-side concentration chamber 42 is formed between the bipolar membrane 33 and the first cation exchange membrane 34, and the first cation exchange membrane 34, anion exchange membrane 35, Between the anion exchange membrane 35 and the second cation exchange membrane 34 ′, an anode side concentration chamber 44 is formed between the second cation exchange membrane 34 ′ and the anode 32. An anode chamber 45 is formed between them.

  The bipolar membrane 33 has a structure in which an anion exchange membrane 33A on the cathode 31 side and a cation exchange membrane 33B on the anode 32 side are bonded together.

  The bipolar membrane used in the present invention is not particularly limited as long as it has an anion exchange membrane and a cation exchange membrane and has high water electrolysis efficiency.

  The cathode side concentration chamber 42 and the anode chamber 45 are filled with a cation exchange resin 38. The anode side concentration chamber 44 is filled with an anion exchange resin 39.

  The cathode chamber 41 is filled with a conductor 36. It is not necessary to exchange ions in the cathode chamber 41, and the cathode chamber 41 only needs to have a space in the cathode chamber 41 for allowing the electrolytic gas generated by water electrolysis to escape upward. As such, a conductor such as a corrosion-resistant conductive metal, for example, stainless steel may be used. Further, the shape of the conductor is not particularly limited as long as the energization resistance does not increase, and may be granular, porous, fibrous, etc. Among them, stainless steel fibers are preferably used.

  The desalting chamber 43 is filled with an ion exchange resin 37 obtained by mixing a cation exchange resin and an anion exchange resin in a mixed bed type. However, a laminated type in which the cation exchange resin 38 and the anion exchange resin 39 are alternately arranged may be used.

  An inlet for raw water (condensed water) is provided at one end of the desalting chamber 43, and an outlet for pure water generated by deionization is provided at the other end.

In this reference example , the main part of pure water flowing out from the desalting chamber 43 is obtained as pure water, and a part of the pure water is collected, and the cathode chamber 41, the cathode side concentration chamber 42, the anode side concentration chamber 44, and the anode chamber 45, respectively. Water.

In order to increase the efficiency of supplying pure water, it is desirable that the replenishment process of the water to be treated (pretreated city water or the like) is completed in as short a time as possible and returned to the normal operation process. Therefore, it is preferable that the water flow rate of the water to be treated to the desalting chamber in the replenishment process is high, for example, SV20 [h ⁻¹ ] or more. However, when SV100 [h ⁻¹ ] is exceeded, desalting of the water to be treated is not sufficiently performed. Therefore, SV is preferably 20 to 100 [h ⁻¹ ].

  In supplying the treated water to the desalting chamber at such a water flow rate, since the ion exchange resin in the desalting chamber is a mixed bed type or a laminated type, the direction of water flow to the desalting chamber of the treated water is A downward flow is preferred. If the water flows in the upward flow, the arrangement of the resin filled in the mixed bed type or the laminated type may be broken, which is not preferable.

  Pipes having valves are connected to the inlets and outlets of the respective chambers 41 to 45, and the flow of water to the respective chambers is controlled by opening and closing the valves and switching the flow paths. The valve control means and the energization control means constitute the operation execution means of the pure water production apparatus. This operation execution means may be operated manually or by a computer or the like.

  In this electrodeionization apparatus, by making the filling structure of the ion exchange resin into a laminated type, the electrical resistance during energization is reduced, so that the processing efficiency is improved and the apparatus can be miniaturized. Therefore, the laminated type is more preferable than the mixed bed type. In this case, each layer of the laminated anion resin and cation resin mixture is preferably a pure anion resin layer or a cation resin layer. However, an anion-rich resin layer or a cation-rich layer may be used as long as the voltage does not increase excessively. It may be a resin layer.

Moreover, in the case of a laminated type, it is preferable that the cation exchange resin → anion exchange resin → cation exchange resin → anion exchange resin →. If the anion exchange resin is the most upstream, OH ions generated in the ion exchange treatment operation mode may react with Mg ions contained in the water to be treated, and Mg (OH) ₂ scale may be produced in the anion exchange resin. Because there is.

Next, the operation mode of this apparatus will be described.
<Electrodeionization operation mode>
In one aspect of this electric deionization operation mode, raw water (condensed water) is introduced into the demineralization chamber 43 while being energized and taken out as pure water. As described above, the main part of the pure water is obtained as pure water, and a part thereof is collected and passed through the cathode chamber 41, the cathode side concentration chamber 42, the anode side concentration chamber 44, and the anode chamber 45, respectively. The cations in the raw water permeate the first cation exchange membrane 34 and move to the cathode side concentrating chamber 42 where they are mixed into the concentrating chamber effluent and discharged. Anions in the raw water permeate the anion exchange membrane 35 and move to the anode side concentrating chamber 44 where they are mixed and discharged into the concentrating chamber effluent.
<Ion exchange treatment operation mode>
In order to produce pure water by ion exchange treatment using this electrodeionization apparatus, as shown in FIG. ^2, in a state where the energization is stopped or the energization is controlled so that the current density is 1000 mA / dm ² or less, The treated water is passed through the desalting chamber 43, and the effluent is obtained as pure water. If the current density exceeds 1000 mA / dm ² , it is presumed that ions that cause scale generation are condensed on the surface of the ion exchange membrane, which may cause the scale to adhere to the surface of the ion exchange membrane. For the same reason, the current density is more preferably 600 mA / dm ² or less. However, it is most preferable to stop energization because scale generation can be reliably prevented and the energization amount can be easily controlled.

<Alternate operation>
After performing the pure water production operation by ion exchange, the process returns to the pure water production operation by electrodeionization. Thereby, the ion exchange resin can be electrically regenerated.

  In the middle of this electrodeionization operation mode, when the amount of pure water retained in the fuel cell power generation device has decreased, ion exchange operation is performed to replenish pure water, and then the electrodeionization operation mode returns.

<Use of fuel cell power generator as pure water supply system>
In this case, prior to on-site installation of the electrodeionization apparatus, it is preferable to test-run the electrodeionization apparatus and regenerate the ion exchange resin in each chamber to start up the electrodeionization apparatus.

  After installation at the site, water is passed as shown in FIG. 2 to produce pure water, and the fuel cell power generator is activated using this pure water. After startup, the electrodeionization apparatus is operated for electrodeionization.

  The treated water supplied to the electrodeionization apparatus at the time of startup is preferably pretreated with city water, well water, industrial water, etc., and at least dechlorination treatment and turbidity treatment are performed as pretreatment. Specifically, for example, activated carbon treatment and membrane filtration such as microfiltration or ultrafiltration are performed.

  In this electrodeionization apparatus, a cathode chamber 41 is provided separately from the cathode-side enrichment chamber 42, and both are separated by a bipolar membrane 33. Therefore, Ca ions and Mg from the cathode-side enrichment chamber 42 to the cathode chamber 41 are removed. The movement of cations such as ions is blocked, and the movement of anions such as hydroxide ions and hydrogen carbonate ions from the cathode chamber 41 to the cathode side concentration chamber 42 is blocked. For this reason, in the cathode chamber 41 or the cathode side concentrating chamber 42, it is possible to prevent the Ca ions, Mg ions, and the like from being associated with hydroxide ions and the like to generate scale.

<Implementation of the form>
FIG. 3 is a system diagram showing an operation example of the ion exchange processing operation mode according to the embodiment using the electrodeionization apparatus of FIG.

  In FIG. 3, the water to be treated is passed through the cathode side concentrating chamber 42, and the outflow water of the cathode side concentrating chamber 42 is obtained as pure water. The reason why the water to be treated is not passed through the desalting chamber 37 is that the ion exchange resin in the desalting chamber 37 is not soiled.

  According to the operation example in the ion exchange treatment operation mode of FIG. 3, cations such as Ca ions and Mg ions in the water to be treated are captured by the cation exchange resin 38 in the cathode side concentration chamber 42.

  As shown in FIG. 4, the pure water that has flowed out of the cathode side concentrating chamber 42 may be further passed through the anode side concentrating chamber 44. Thereby, the anion in the pure water is captured by the anion exchange resin 39 in the anode side concentration chamber 44. However, if water is passed through the two chambers in this way, the pressure loss is large and the load applied to the pump increases. Therefore, it is preferable that water is passed through the two chambers only when necessary.

  Further, in FIG. 3, the cathode side concentrating chamber 42 is filled with the cation exchange resin 38. However, the cathode side concentration chamber 42 may be filled with a laminated type in which anion exchange resin and cation exchange resin are alternately arranged. May be filled. In this case, the anion and the cation are removed by passing the water to be treated through one chamber of the cathode side concentration chamber 42.

  Although the bipolar membrane 33 is used in the above embodiment, a monovalent cation selective permeable cation exchange membrane may be used instead of the bipolar membrane 33. Even in this case, when the water to be treated is passed through at least one of the desalting chamber 43, the cathode chamber side concentration chamber 42, and the anode chamber side concentration chamber 44 in the ion exchange processing operation mode, the cathode side concentration chamber The movement of cations such as Ca ions and Mg ions from 42 to the cathode chamber 41 is blocked, and the movement of anions such as hydroxide ions and hydrogen carbonate ions from the cathode chamber 41 to the cathode side concentration chamber 42 is blocked. The For this reason, in the cathode chamber 41 or the cathode side concentrating chamber 42, it is possible to prevent the Ca ions, Mg ions, and the like from being associated with hydroxide ions and the like to generate scale. Monovalent cations such as sodium ions can permeate the monovalent cation selective permeable cation exchange membrane.

  Currently, in the boiler water supply treatment, soft water is mainly used as make-up water treatment, and pure water equipment is used as condensate treatment. The present invention can be equipped with the functions of both of these devices in a single unit. That is, it is possible to replenish city water with pure water purified by the present invention when replenishing boiler water, and to replenish pure water with the present invention even when condensate is purified during boiler operation. By applying the present invention, the apparatus can be miniaturized, and salt water replenishment for the water softener and acid / alkali regeneration wastewater treatment from the deionized water apparatus can be dispensed with, thereby contributing to a reduction in environmental load.

  Hereinafter, examples and comparative examples will be described. In this embodiment, a five-chamber electrodeionization apparatus is used to produce pure water by electrodeionization using the water flow system shown in FIG. 1, and city water purification (ion exchange) is performed using the water flow system shown in FIG. Treatment).

  In the electrodeionization apparatus, the thickness of the demineralization chamber 43 was 5 mm, and the thickness of the other four chambers 41, 42, 44, 45 was 2.5 mm. Further, the height of each of the exchange membranes 33, 34, 34 ', and 35 was set to 200 mm.

[Example]
1) Startup of electrodeionization apparatus Pure water having a resistivity of 1 MΩ · cm was supplied to the desalting chamber 43 at 2.3 L / h, and 2 L / h of the desalting chamber outlet water was obtained as production water. The remaining 0.3 L / h was divided into four equal parts and supplied to the remaining chambers, and each outlet water was drained. A 0.1 A direct current was applied to the electrode to start water flow, and when the production water reached 16 MΩ · cm, the start-up was completed.

2) City water purification (ion exchange treatment)
The necessary city water purification was performed with the cation exchange resin 38 filled in the cathode side concentration chamber 42 and the ion exchange resin 39 filled in the anode side concentration chamber 44.

  First, city water was dechlorinated with activated carbon, turbidized with a precision filter, and supplied to the cathode side concentration chamber 42 at 0.3 L / h. Subsequently, the outlet water of the cathode side concentration chamber 42 was supplied to the anode side concentration chamber 44. When the resistivity of the outlet water of the anode side concentrating chamber 44 was measured, the water quality was approximately 5 MΩ · cm, and about 1.0 L of pure water was obtained. In addition, electricity was stopped while purifying the city water.

3) Simulated condensate purification (electric deionization)
Simulated water of condensate obtained from the fuel cell was prepared as raw water, and subjected to electrodeionization treatment with an electrodeionization apparatus that purified the city water in 2). The simulated solution was prepared by dissolving sodium chloride and carbon dioxide in pure water so that the electric conductivity was about 1 mS / m.

  Simulated water was supplied to the desalting chamber 43 and treated by passing water under the same conditions as in the above 1), including application of DC voltage. As a result, a water quality of 15 MΩ · cm could be obtained.

  The simulated condensed water was passed for about one week. During this time, pure water with good water quality was obtained.

4) Repeated municipal water purification and simulated condensate purification Step 3) After simulated condensed water purification, step 2) municipal water purification and step 3) simulated condensed water purification were alternately performed and repeated a total of 5 times. By repeating 5 times, the amount of pure water obtained by purification of city water gradually decreased, but the amount of pure water obtained at the 5th time was about 75% of the first time and was practical.

  The quality of pure water obtained by purifying simulated condensate was as good as about 15 MΩ · cm, and the electrodeionization function was good, and pure water could be obtained continuously.

  Furthermore, although the test was continued, deposition of scale on the surface of the ion exchange membrane in the cathode chamber 41, the cathode 31 surface, the cathode side concentration chamber 42, etc. was not confirmed.

[Comparative example]
Except that the bipolar membrane 33 was replaced with a cation exchange membrane, the performance was examined by supplying the same volume of city water and simulated condensed water using an electrodeionization apparatus having the same configuration as in the example.

  As a result, the quality of the pure water obtained by purifying the simulated condensed water was as good as about 15 MΩ · cm, the electrodeionization function was good, and pure water could be obtained continuously.

  However, when the test was continued, deposition of scale was confirmed on the cathode surface in the cathode chamber.

It is a schematic longitudinal cross-sectional view of the electric deionization apparatus which concerns on a reference example . It is a systematic diagram which shows the example of a pure water manufacture driving | operation by the ion exchange system using the electrodeionization apparatus of FIG. It is a systematic diagram which shows another example of a pure water manufacturing operation by the ion exchange system using the electrodeionization apparatus of FIG. It is a systematic diagram which shows another example of a pure water manufacturing operation by the ion exchange system using the electrodeionization apparatus of FIG. It is a systematic diagram of the fuel cell power generator concerning a conventional example.

31 Cathode 32 Anode 33 Bipolar Membrane 34 First Cation Exchange Membrane 34 ′ Second Cation Exchange Membrane 35 Anion Exchange Membrane 36 Conductor 37 Ion Exchange Resin 38 Cation Exchange Resin 39 Anion Exchange Resin 41 Cathode Chamber 42 Concentration Chamber on the Cathode Chamber Side 43 Desalination chamber 44 Anode chamber side enrichment chamber 45 Anode chamber

Claims (9)

By disposing an ion exchange membrane between the anode and the cathode, at least a cathode chamber, a cathode-side concentration chamber, a desalting chamber, and an anode-side concentration chamber are provided, the cathode chamber is filled with a conductor, and the cathode-side concentration is performed. In a pure water production apparatus having an electrodeionization apparatus comprising an ion exchanger filled in a chamber, the demineralization chamber and the anode-side concentration chamber,
The ion exchange membrane that partitions the cathode chamber and the cathode chamber-side concentration chamber is a bipolar membrane or a monovalent cation selective permeable cation exchange membrane,
Provided with means for executing an ion-exchange-type pure water production operation mode in which treated water is passed through at least one concentration chamber, ion exchange is performed by an ion exchanger in the concentration chamber, and pure water is discharged from the concentration chamber. An apparatus for producing pure water. 2. The pure water production according to claim 1 , wherein the means for executing the ion-exchange-type pure water production operation mode includes an energization control means for stopping energization or adjusting a current density to 1000 mA / dm ² or less. apparatus. 3. In the ion exchange type pure water production operation mode according to claim 1 , wherein water to be treated is passed through the cathode side concentrating chamber and then through the anode side concentrating chamber. Pure water production equipment. The mixed bed of an anion exchanger and a cation exchanger as an ion exchanger is filled in at least one of the cathode chamber side concentrating chamber and the anode chamber side concentrating chamber according to any one of claims 1 to 3. Alternatively, at least one of the cathode chamber side concentrating chamber and the anode chamber side concentrating chamber is filled with a cation exchanger and an anion exchanger alternately in this order from the upstream side. . In any one of claims 1 to 4, wherein the conductor includes a pure water production apparatus which is a cation exchanger or corrosion resistant conductive metal body. By disposing an ion exchange membrane between the anode and the cathode, at least a cathode chamber, a cathode-side concentration chamber, a desalting chamber, and an anode-side concentration chamber are provided, the cathode chamber is filled with a conductor, and the cathode-side concentration is performed. A method for producing pure water using an electrodeionization apparatus comprising a chamber, the demineralization chamber and the anode-side concentration chamber filled with an ion exchanger,
The ion exchange membrane that partitions the cathode chamber and the cathode chamber-side concentration chamber is a bipolar membrane or a monovalent cation selective permeable cation exchange membrane,
Purified water is supplied through at least one concentration chamber, ion exchange is performed by an ion exchanger in the concentration chamber, and pure water is discharged from the concentration chamber. Water production method. 7. The pure water production according to claim 6 , wherein the ion exchange type pure water production operation is performed in a state where energization is stopped or the energization is controlled so that the current density is 1000 mA / dm ² or less. Method. 8. The pure water manufacturing method according to claim 6 or 7 , wherein the water to be treated is city water, well water, or industrial water that has been subjected to turbidity treatment and dechlorination treatment. In any one of Claims 6 thru | or 8 , the said electrodeionization apparatus is for the purification of the recovered water of a fuel cell power generation apparatus,
A method for producing pure water, comprising producing ion-exchanged pure water by the electrodeionization device when the fuel cell power generator is started up, and supplying the produced pure water to the fuel cell power generator.

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