JP2008161761A - Pure water making method and pure water making apparatus - Google Patents

Abstract

<P>PROBLEM TO BE SOLVED: To perform both the production of pure water due to electric deionization and the production of pure water due to ion exchange using an electric deionizing apparatus. <P>SOLUTION: In a pure water making apparatus having the electric deionizing device constituted by providing a concentration chamber and cathode chamber 35, a desalting chamber 37 and an anode-side concentration chamber 40 by arranging ion exchange films 33', 34 and 33 between an anode 32 and a cathode 31 and filling the respective chambers with ion exchange resins, water to be treated is passed through the desalting chamber 37 in the state that the supply of a current is stopped or controlled so that current density becomes 1,000 mA/dm<SP>2</SP>or below and subjected to ion exchange by the ion exchange resins 38 and 39 in the desalting chamber 37 to allow pure water to flow out of the desalting chamber 37. <P>COPYRIGHT: (C)2008,JPO&INPIT

Description

  The present invention relates to a pure water production apparatus. Preferably, the present invention recovers the steam generated by the power generation reaction and the condensed water of the steam in the combustion exhaust gas in the reformer, and uses the recovered water as a steam source for steam reforming. The present invention relates to a pure water production apparatus for a fuel cell power generator provided with an ion device. 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. 4 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 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. 4, 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. 4, 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.

By the way, the present applicant proposed in JP-A-2004-82092 an electrodeionization apparatus capable of flowing a necessary amount of current and sufficiently performing membrane ion treatment even when the applied voltage between the electrodes is lowered. Yes.
JP 2001-176535 A JP 2004-82092 A

  As shown in FIG. 4 above, when the fuel cell power generator recovered water is treated with water in the electrodeionization apparatus to produce pure water and supply it to the fuel cell, the fuel cell power generator is operated when the fuel cell power generator is started up. 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.

The pure water production apparatus according to claim 1 is provided with at least a cathode side concentration chamber, a desalting chamber, and an anode side concentration chamber by disposing an ion exchange membrane between an anode and a cathode, and an ion exchanger is provided in each chamber. In a pure water production apparatus having an electrodeionization apparatus that is filled, the water to be treated is passed through the demineralization chamber 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. And an ion exchange type pure water production operation mode executing means for exchanging ions with an ion exchanger in the desalting chamber and allowing pure water to flow out of the desalting chamber.

  The pure water production apparatus according to claim 2 is the pure water production apparatus according to claim 1, wherein the electrodeionization apparatus includes a first cation exchange membrane, an anion exchange membrane, and a second cation exchange membrane between a cathode and an anode. Are arranged in this order, a concentration chamber / cathode chamber is provided between the cathode and the first cation exchange membrane, and a desalting chamber is provided between the first cation exchange membrane and the anion exchange membrane, An electrodeionization apparatus in which a concentration chamber is provided between the anion exchange membrane and the second cation exchange membrane, and an anode chamber is provided between the second cation exchange membrane and the anode. It is a feature.

  The pure water production apparatus according to claim 3 is characterized in that, in claim 1 or 2, the demineralization chamber is alternately filled with a cation exchanger and an anion exchanger in this order from the upstream side. is there.

According to a fourth aspect of the present invention, there is provided a method for producing pure water comprising disposing an ion exchange membrane between an anode and a cathode, thereby providing at least a cathode-side concentrating chamber, a desalting chamber, and an anode-side concentrating chamber. In a method for producing pure water using a charged electrodeionization apparatus, water to be treated is put into the demineralization chamber in a state in which energization is stopped or the energization is controlled so that the current density is 1000 mA / dm ² or less. An ion-exchange-type pure water production operation is performed in which pure water is flowed out and ion-exchanged by an ion exchanger in the desalting chamber to flow out pure water from the desalting chamber.

  The pure water production method according to claim 5 is characterized in that, in claim 4, the water to be treated is city water, well water, or water obtained by removing turbidity and dechlorination from industrial water. .

  According to a sixth aspect of the present invention, there is provided a pure water production method according to the fourth or fifth aspect, wherein the electrodeionization device is for purifying the recovered water of the fuel cell power generation device, and is activated by the electrodeionization device when starting the fuel cell power generation device. Ion exchange type pure water production is performed, and the produced pure water is supplied to the fuel cell power generator.

  According to the pure water production apparatus of claim 1 and the pure water production method of claim 4, 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, by keeping the energization amount below the specified amount, the ions that cause scale formation in the water to be treated are difficult to concentrate near the surface of the cathode and ion exchange resin, so scale adheres to the cathode and ion exchange resin. Can be prevented.

  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.

  The electrodeionization apparatus used in the pure water production apparatus according to the second aspect is the electrodeionization apparatus described in JP-A-2004-82092, and is sufficiently ionized even when the applied voltage between the electrodes is lowered. It is possible to produce ion-treated pure water.

  This electrodeionization apparatus has one desalination chamber, and an anode side concentrating chamber and a cathode / concentration chamber are arranged on both sides of the desalting chamber, respectively. Since the chamber is arranged, the distance between the electrodes is small and the applied voltage between the electrodes is low.

In this electrodeionization apparatus, an anode chamber is provided separately from the anode-side enrichment chamber, and both are separated by a second cation exchange membrane, so that Cl ⁻ ions move from the anode-side enrichment chamber to the anode chamber. Is blocked. Therefore, Cl ₂ generated in the anode chamber is derived only from Cl ⁻ in the electrode water introduced into the anode chamber, so that the amount of Cl ₂ generated in the anode chamber is extremely small. For this reason, the conductor such as the cation exchange resin filled in the anode chamber and the second cation exchange membrane facing the anode chamber are prevented from being deteriorated by Cl ₂ .

  It is preferable that the desalting chamber through which the water to be treated is passed for producing pure water by ion exchange treatment is alternately filled with the cation exchanger and the anion exchanger from the upstream side. The advantages of the alternate lamination method will be described in detail later with reference to the drawings.

  Hereinafter, embodiments will be described with reference to the drawings. FIG. 1 is a schematic longitudinal sectional view of an electric deionization apparatus according to an embodiment.

  Between the cathode 31 and the anode 32, the first cation exchange membrane 33, the anion exchange membrane 34, and the second cation exchange membrane 33 ′ are arranged one by one, and the cathode 31 and the first cation exchange membrane are arranged. 33, a concentration chamber / cathode chamber 35 is formed between the first cation exchange membrane 33 and the anion exchange membrane 34, and a desalting chamber 37 is formed between the anion exchange membrane 34 and the second cation exchange membrane. A concentration chamber 40 is formed between the second cation exchange membrane 33 ′ and the anode 32, and an anode chamber 36 is formed between the second cation exchange membrane 33 ′ and the anode 32.

  The concentration chamber / cathode chamber 35 and the anode chamber 36 are each filled with a cation exchange resin 38. The concentration chamber 40 is filled with an anion exchange resin 39. The desalting chamber 37 is filled with cation exchange resin 38 and anion exchange resin 39 so as to be alternately stacked in the flow direction, and the cation exchange resin is arranged on the most upstream side.

  An inlet of raw water is provided at one end of the desalting chamber 37, and an outlet of deionized water is provided at the other end.

  One end of the anode chamber 36 is provided with an inlet for raw water or deionized water. Outflow water from the anode chamber 36 flows into the concentration chamber 40 from one end side and flows out from the other end side. The outflow water of the concentration chamber 40 flows into the concentration chamber / cathode chamber 35 from one end side and is discharged from the other end side as concentrated water / cathode electrode 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.

  A pipe having a valve is connected to the inlet and outlet of each of the chambers 35, 37, 40, and 36, and water flow to each chamber is controlled by opening and closing of the valve and switching of the flow path. 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 mode of this electric deionization operation mode, as shown in FIG. 1, raw water (condensed water) is introduced into the demineralization chamber 37 in an energized state and taken out as pure water. As described above, pure water is introduced into the anode chamber 36, and sequentially flows through the concentration chamber 40 and the concentration chamber / cathode chamber 35. The cations in the raw water pass through the first cation exchange membrane 33 and are mixed with the cathode electrode water and discharged.

  In addition, it is good also as FIG. 2 as a water flow aspect which performs an electrodeionization driving | operation.

  In FIG. 2, the raw water (condensed water) is passed through the desalting chamber 37, the main part of the effluent of the desalting chamber 37 is obtained as pure water, and a part of it is separated, and the concentrating chamber / cathode chamber respectively. 35, water is passed through the concentration chamber 40 and the anode chamber 36.

<Ion exchange treatment operation mode>
In order to produce pure water by ion exchange treatment using this electrodeionization apparatus, as shown in FIG. 3, 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 37, and the effluent water 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 cathode or ion exchange membrane, which may cause the scale to adhere to the surface of the cathode or ion exchange membrane. Absent. 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, pure water is produced by passing water as shown in FIG. 3, and the fuel cell power generator is started using the 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.

<Other forms>
The above-mentioned electrodeionization apparatus has a four-chamber structure of chambers 35, 37, 40, and 36. However, an electrodeionization apparatus having a three-chamber structure of a concentration chamber / cathode chamber, a desalting chamber, and a concentration chamber / anode chamber is used. It may be used.

  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 example and comparative example, pure water was produced by electrodeionization using a four-chamber structure electrodeionization apparatus by the water flow method shown in FIG. Moreover, the city water purification in the examples was carried out by the water flow method shown in FIG.

[Example]
1) Startup of electrodeionization apparatus Pure water having a resistivity of 1 MΩ · cm was supplied to the desalting chamber 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 three 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 an ion exchange resin filled in the desalting chamber.

  First, city water was dechlorinated with activated carbon, then turbidized with a precision filter, and supplied to a desalting chamber at 0.3 L / h. When the resistivity of the outlet water of the desalting chamber was measured, the water quality was approximately 6 MΩ · cm, which was good, 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 a fuel cell was prepared as raw water, and was 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 and treated by passing water under the same conditions as in 1) above, including application of DC voltage. As a result, water quality of 6 MΩ · cm equivalent to that at the time of city water purification 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) Repeating of city water purification and simulated condensate purification Step 3) After purifying simulated condensate, Step 2) City water purification and Step 3) Simulated condensate 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 70% of the first time and was practical.

  The quality of pure water obtained by purifying simulated condensate was as good as about 6 MΩ · cm, and the electrodeionization function was good, and pure water could be obtained continuously.

[Comparative example]
About 20 mL of mixed bed ion exchange resin in the same amount as that in the demineralization chamber of the electric deionizer is packed in the column after regeneration, and the same volume of city water and simulated condensate as in the present invention are supplied. The purification performance was investigated. As a result, after the first city water purification, it broke through in the middle of the simulated condensed water purification process and became unusable.

It is a systematic diagram which shows the example of a pure water manufacture driving | operation by the electrodeionization of the electrodeionization apparatus of 4 chamber structure. It is a systematic diagram which shows another example of a pure water manufacture driving | operation by the electrodeionization of the electrodeionization apparatus of FIG. 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 of the fuel cell power generator concerning a conventional example.

Explanation of symbols

31 Cathode 32 Anode 33 First Cation Exchange Membrane 33 ′ Second Cation Exchange Membrane 34 Anion Exchange Membrane 35 Concentration Chamber / Cathode Chamber 36 Anode Chamber 37 Desalination Chamber 38 Cation Exchange Resin 39 Anion Exchange Resin 40 Concentration Chamber

Claims (6)

By providing an ion exchange membrane between the anode and cathode, at least a cathode side concentration chamber, a desalting chamber, and an anode side concentration chamber are provided, and an electrodeionization apparatus is provided in which each chamber is filled with an ion exchanger. In pure water production equipment,
The water to be treated is passed through the desalting chamber in a state where the energization is stopped or the current density is controlled to 1000 mA / dm ² or less, and ion exchange is performed by the ion exchanger in the desalting chamber. An apparatus for producing pure water, comprising means for executing an ion-exchange-type pure water production operation mode for allowing pure water to flow out from the desalting chamber. The electrodeionization device according to claim 1,
Between the cathode and the anode, a first cation exchange membrane, an anion exchange membrane, and a second cation exchange membrane are arranged in this order,
A concentration chamber / cathode chamber is provided between the cathode and the first cation exchange membrane;
A desalting chamber is provided between the first cation exchange membrane and the anion exchange membrane;
A concentration chamber is provided between the anion exchange membrane and the second cation exchange membrane;
An apparatus for producing pure water, which is an electrodeionization apparatus in which an anode chamber is provided between the second cation exchange membrane and the anode.   3. The pure water production apparatus according to claim 1, wherein the desalting chamber is alternately filled with a cation exchanger and an anion exchanger in this order from the upstream side. By using an electrodeionization apparatus in which at least a cathode side concentrating chamber, a desalting chamber, and an anode concentrating chamber are provided by disposing an ion exchange membrane between the anode and the cathode, and each chamber is filled with an ion exchanger. In the method for producing pure water,
The water to be treated is passed through the demineralization chamber in a state where the energization is stopped so that the current density is 1000 mA / dm ² or less, and ion exchange is performed by the ion exchanger in the demineralization chamber. An ion exchange type pure water production operation for flowing pure water out of the desalting chamber is carried out.   7. The pure water production method according to claim 6, wherein the water to be treated is city water, well water, or water obtained by removing turbidity and dechlorination from industrial water. In Claim 4 or 5, the electrodeionization device is for purifying the recovered water of the fuel cell power generator,
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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