JP6916702B2 - Measurement method and measurement system for conductivity of decationized water - Google Patents

Description

The present invention relates to a method and a measuring system for measuring the conductivity of decationized water, and particularly to a method for measuring the conductivity of condensate water in a power plant.

At thermal power plants and nuclear power plants (hereinafter referred to as power plants), high-temperature and high-pressure steam generated by steam generating means such as boilers is introduced into the steam turbine, and the exhaust steam discharged from the steam turbine is used as a condenser. Water circulation is carried out in which condensate is condensed into condensate, and the condensate is supplied to the steam generating means as water supply. Since impurities such as corrosion products accumulate in the condensate, a condensate desalination device is installed at the power plant to remove these impurities from the condensate during steady operation. When the condenser is a seawater cooling system, the condensate desalination device also has a function to protect the condensate system by capturing sodium chloride etc. contained in the seawater that may be mixed in the condensate for a certain period of time. There is. However, if an amount of seawater exceeding a certain amount flows in, it exceeds the operational permissible range of the condensate desalination apparatus. Therefore, the power plant is provided with a conductivity meter for the purpose of detecting the seawater component in the condensate. ..

On the other hand, in power plants, in order to suppress corrosion of condensate piping and the like, a pH adjuster such as ammonia is added to the condensate to make the condensate alkaline. Therefore, the condensate is in a state of low resistivity and high conductivity, and even if a small amount of seawater is mixed in the condensate, the change in resistivity or conductivity is small. Therefore, it is difficult to accurately detect the inclusion of seawater with a conductivity meter. In order to solve this problem, a method may be adopted in which cations such as ammonia are removed in advance with a decationizing ion device and condensate with reduced conductivity is supplied to the conductivity meter (Patent Documents 1 and 2). .. According to this method, the detection accuracy of anions derived from seawater is improved, and the contamination of seawater can be detected with high accuracy.

Patent 467127A Patent 3704289 Gazette

The pH of condensate has been set to about 8.5 to 9.8 in the past, but with the revision of JIS B8223 "Boiler water supply and boiler water quality", it may be operated at a value exceeding 10 in recent years. Along with this, the amount of ammonia or the like added as a pH adjuster is increasing, and the load on the decationizing device is also increasing. In a decationization device using a cation exchange resin, the time required to reach the once-through capacity is shortened, and more frequent replacement of the cation exchange resin and chemical regeneration are required. In the case of an electroregenerative decationizing ion device, this problem does not occur, but the current value is insufficient and ammonia and the like cannot be sufficiently removed. In addition, increasing the current value accelerates the deterioration of the device.

An object of the present invention is to provide a method and a measuring system for measuring the conductivity of decationized water having high decationization efficiency and a small load on an apparatus.

According to one aspect of the present invention, the method for measuring the conductivity of decationized water is to add diluted water to water to be treated containing cations and anions to generate diluted water to be treated with a lowered pH. To generate decationized water by supplying diluted water to be treated to the decationization device, and to supply the decationization water generated by the decationization device to the conductivity meter to remove the cations. It has the ability to measure the conductivity of cationic water. Further, according to one aspect of the present invention, the system for measuring the conductivity of decationized water is a diluted water to be treated in which the pH is lowered by adding diluted water to the water to be treated containing cations and anions. It has a diluting device for generating water, a decationizing device for generating decationized water from diluted water to be treated, and a conductivity meter for measuring the conductivity of the decationized water generated by the decationizing device. ..

According to the present invention, it is possible to provide a method and a measuring system for measuring the conductivity of decationized water having high decationization efficiency and a small load on the apparatus.

It is a conceptual diagram of the conductivity measurement system of decationized water which concerns on 1st Embodiment of this invention. It is a conceptual diagram of the conductivity measurement system of decationized water which concerns on 2nd Embodiment of this invention. It is a conceptual diagram of the conductivity measurement system of decationized water which concerns on 3rd Embodiment of this invention.

Hereinafter, some embodiments of the present invention will be described with reference to the drawings. In each embodiment, the water to be treated is condensate from a thermal power plant or a nuclear power plant. That is, the conductivity measuring system in each embodiment of the present invention is a system provided in a thermal power plant or a nuclear power plant. However, the present invention is not limited to this, and can be applied to methods and systems for measuring the conductivity of decationized water produced by a decationized ion device.

(First Embodiment)
FIG. 1 shows a conceptual diagram of a conductivity measurement system 1 (hereinafter referred to as system 1) for decationized ionized water according to the first embodiment of the present invention. The system 1 includes a decationization ion device 3, a conductivity meter 4, a flow meter 2, and a valve 7. These devices are installed on the pipe 6 branching from the water recovery pipe 8. The outlet of the conductivity meter 4 is connected to the drain pipe 9. In addition, the system 1 has a diluting device 10. The diluting device 10 includes a diluting water supply line 11 that branches from the drain pipe 9 and is connected to the pipe 6, and a transfer pump 12, a valve 13, and a flow meter 14 provided on the diluting water supply line 11. The condensate supplied from the condensate pipe 8 is diluted with the diluting water supplied from the diluting device 10 to become diluted water to be treated. The decationizing ion device 3 generates decationized water from diluted water to be treated containing cations and anions. The conductivity meter 4 measures the conductivity of the decationized water generated by the decationizing ion device 3. The flow meter 2 measures the flow rate of the diluted water to be treated flowing into the decationization ion device 3. The valve 7 is normally open, but is closed when the system 1 needs to be isolated from the condensate system.

The decationization ion device 3 has a desalination chamber 31 and a pair of concentration chambers 32 and 33 arranged on both sides of the desalination chamber 31 via cation exchange membranes 34 and 35. A positive electrode 36 is arranged in the concentrating chamber 32, a negative electrode 37 is arranged in the concentrating chamber 33, and the concentrating chambers 32 and 33 also serve as electrode chambers. The positive electrode 36 and the negative electrode 37 are connected to the DC power supply 38. The desalting chamber 31 is filled with a cation exchanger 39. The composition of the cation exchanger 39 is not limited as long as it can capture and remove the cation component, but is a cation exchange resin, a monolithic porous cation exchanger (hereinafter, simply referred to as “monolith”), or a fibrous porous cation exchanger. , A particle-aggregated porous ion exchanger can be preferably used.

The monolith has an open cell structure having mesopores having an average diameter of 1 to 1000 μm, preferably 10 to 100 μm in the walls of the macropores connected to each other, and the total pore volume is 1 to 50 ml / g, preferably. Is 4 to 20 ml / g, the ion exchange group is uniformly distributed, and the ion exchange capacity is 0.5 mg equivalent / g or more of the dry porous body. Other physical properties of the monolith and a method for producing the monolith are disclosed in, for example, Japanese Patent Application Laid-Open No. 2003-334560.

If a monolith is used as the cation exchanger, the pore volume and specific surface area can be significantly increased. Therefore, the deionization efficiency of the electroregenerative decationization device is remarkably improved, which is very advantageous. Further, if the total pore volume of the monolith is less than 1 ml / g, the amount of water flowing per unit cross-sectional area becomes small, which is not preferable because the processing capacity is lowered. On the other hand, if the total pore volume exceeds 50 ml / g, the proportion occupied by the skeleton portion decreases, and the strength of the porous body decreases significantly, which is not preferable. When a monolith having a total pore volume of 1 to 50 ml / g is used as an ion exchanger of an electroregenerative decationizing device, both the strength of the porous body and the deionizing efficiency can be satisfied. Is preferable. Further, if the ion exchange capacity of the monolith is less than 0.5 mg equivalent / g dry porous body, the ion adsorption capacity is insufficient, which is not preferable. Further, if the distribution of ion exchange groups is non-uniform, the ion movement in the porous cation exchange body becomes non-uniform, which hinders the rapid elimination of adsorbed ions, which is not preferable.

Examples of the fibrous porous ion exchanger include single fibers and woven fabrics and non-woven fabrics which are aggregates of single fibers described in JP-A-5-64726, and ions by utilizing radiation graft polymerization on these processed products. Examples thereof include those that have been processed and molded by introducing an exchange group. Further, as the particle-aggregating porous ion exchanger, for example, a mixed polymer of a thermoplastic polymer and a thermosetting polymer described in JP-A-10-192716 and JP-A-10-192717, or a crosslinkable polymer is used. Examples thereof include those obtained by binding ion exchange resin particles and processing and molding them.

The decationization device 3 of the present embodiment is an electric regeneration type decationization ion device (EDI). In EDI, cation components (Na ⁺ , Ca ²⁺ , Mg ^2+, etc.) are captured by the cation exchanger 39, and at the same time, a water dissociation reaction occurs in the desalting chamber 31, and hydrogen ions and hydroxide ions are generated. appear. The cation component trapped in the cation exchanger 39 is exchanged for hydrogen ions and released from the cation exchanger 39. The liberated cation component is electrophoresed through the cation exchanger 39 to the cation exchange membrane 35 on the negative electrode 37 side, electrodialyzed by the cation exchange membrane 35, and moved to the concentration chamber 33. The cationic component that has moved to the concentration chamber 33 is discharged together with the concentrated water flowing through the concentration chamber 33. After the exchange group of the cation exchanger 39 is bonded to the cation component, the cation component is released and recombined with the hydrogen ion, so that the cation exchanger 39 is continuously regenerated. As described above, in EDI, since the removal of the cation component and the regeneration of the cation exchanger 39 are automatically and continuously performed, it is basically unnecessary to perform the regeneration of the cation exchanger 39 in a separate step. The decationization device 3 is not limited to EDI, and may be an electrodialysis device (ED) that is not filled with the cation exchanger 39. Further, the decationization ion device 3 may be a cation exchange tower filled with a cation exchange resin. When the water flow load reaches the exchange capacity, the cation exchange tower regenerates the cation component (cation) contained in the diluted water to be treated by regenerating with a chemical such as hydrochloric acid.

Hereinafter, the operation method of the system 1 will be described. During operation of the power plant, condensate is flowing through the condensate pipe 8. The valve 7 is opened and the condensate is introduced into the decationization ion device 3 through the pipe 6. Further, the decationized ionized water discharged from the conductivity meter 4 is supplied to the pipe 6 via the transfer pump 12, the valve 13, and the flow meter 14. Therefore, the condensate (water to be treated) supplied from the condensate pipe 8 is diluted with decationized water to become diluted water to be treated. The flow rate of the diluted water to be treated introduced into the decationization device 3 is measured by a flow meter 2 installed upstream of the decationization ion device 3.

Condensate (water to be treated) contains ammonia and hydrazine to prevent corrosion of condensate piping and equipment. These are pH regulators added to the condensate to adjust the pH of the condensate. The pH of condensate was about 8.5 (ammonia 1 mg / L) to 9.8 (ammonia 5 mg / L) in conventional thermal power plants, but in recent years it may be operated at 10 or more. Ammonia is usually present in the condensate in the form of ^{NH +} or NH _3. The cations in the water to be treated are captured by the cation exchanger 39 of the decationizer 3 and discharged to the concentration chamber 33 on the negative electrode 37 side through the cation exchange membrane 35. The treated water from which the cation component has been removed by the decationizing ion device 3 is in a state of substantially pure water. Therefore, the conductivity of the treated water measured by the conductivity meter 4 is 0.1 μS / cm or less.

Seawater may be mixed into the condensate system connected to the condensate of the seawater cooling system. That is, since the steam side is decompressed in the condenser, if a pinhole or the like occurs in the thin tube through which the seawater flows in the condenser, the seawater invades the steam side from the thin tube and the salt concentration of the condensed water increases significantly. do. Examples of the salt contained in seawater include NaCl, Na ₂ SO _{4 and the} like. When condensate salts thereof are mixed is introduced into decationizing device 3, Na ⁺ is trapped by the cation exchanger 39, Cl ^-, treated water, including SO ₄ ^-2 from decationizing device 3 It is discharged. The conductivity meter 4 detects _{HCl and H 2} SO _4. Therefore, the conductivity of the treated water measured by the conductivity meter 4 becomes a value larger than usual (for example, 0.1 μS / cm or more). In this way, most of the cations are removed, and by measuring the conductivity of the treated water containing anions derived from seawater such as chloride ions with the conductivity meter 4, it is possible to detect the contamination of seawater into the condensate. can. Such a conductivity meter 4 is sometimes called an acid conductivity meter.

As described above, when the pH of the water to be treated is high, the load on the decationizing ion device 3 becomes high. When the decationizer 3 is EDI, the cation exchanger is continuously regenerated, so that the chemical regeneration of the cation exchanger is unnecessary even if the load is high. However, since there are many cations to be removed, the current is insufficient and the cations cannot be removed in a short time. Increasing the voltage to increase the current may accelerate the deterioration of the decationizing ion device 3. There is a similar problem with ED. In the case of a cation desalting column, the cation exchange resin saturates quickly, so that the frequency of resin exchange and regeneration increases.

On the other hand, in the present embodiment, since the condensate introduced from the condensate pipe 8 is diluted with the decationized ionized water, it is possible to suppress an increase in the load of cations in the decationized ion apparatus 3. For example, when the pH of the pure water diluted solution of ammonia is 9.7 (hereinafter referred to as a comparative example), the concentration of ammonia is 0.9 mg / L, and when the pH is 10.3, the concentration of ammonia is 3. It becomes 0.6 mg / L, which increases four-fold. Therefore, if the condensate having a pH of 10.3 is diluted 4-fold and the flow rate of the diluted water to be treated supplied to the decationization device 3 is the same as that of the comparative example, the load of the decationization device 3 will be increased. It will be almost the same as the load when treating the condensate in the comparative example. In this case, the opening degrees of the valves 7 and 13 may be adjusted so that the ratio of the flow rate of the condensate water introduced from the condensate pipe 8 to the flow rate of the diluted water is 1: 3. The opening degree of the valves 7 and 13 can be controlled based on the measured values of the flow meters 2 and 14. The flow rate ratio can also be adjusted by adjusting the output of the transfer pump 12. Of the decationized water discharged from the conductivity meter 4, about 1/2 to 3/4 of the total is used as diluted water, and the remaining decationized water is used as electrode water and used as concentrated water. Will be discarded. In the case of the above example, the flow rate of the diluted water to be treated supplied to the decationization ion device 3 is preferably about the same as that of the comparative example, but may be smaller than that of the comparative example. The permissible flow rate of the conductivity meter 4 has a certain range, and there is no problem even if the flow rate of the diluted water to be treated supplied to the decationizing ion device 3 decreases with respect to the comparative example within the permissible flow rate. When the flow rate of the diluted water to be treated to be supplied to the decationization device 3 is smaller than that of the comparative example, it is desirable to confirm whether or not a drift is generated in the decationization ion device 3.

^{The concentration of the ion to be detected (Cl −} ion, etc.) contained in the diluted water to be treated supplied to the conductivity meter 4 becomes smaller than that in the comparative example due to dilution, but the sensitivity of the conductivity meter 4 is sufficiently high, so that seawater leaks. It is possible to secure the sensitivity required for the detection of. For example, when NaCl having a concentration of 100 μg / L is mixed in condensate due to seawater leakage, the conductivity detected by the condensate meter 4 before dilution (condensation detected as decationized HCl). ) Is 0.73 μS / cm. Even when diluted 5 times, the conductivity of the diluted water to be treated is 0.16 μS / cm, which can be sufficiently measured with an existing conductivity meter.

As the diluting water, it is preferable to use the wastewater of the conductivity meter 4 from the viewpoint of minimizing additional equipment, but for example, pure water supplied from the pure water supply system of the power plant may be used. The diluted water preferably contains as little cations as possible, but water having a lower cation concentration than the water to be treated (low cation concentration water) may be used.

(Second embodiment)
FIG. 2 shows a conceptual diagram of a conductivity measuring system 101 (hereinafter referred to as system 101) for decationized water according to a second embodiment of the present invention. In the following description, a configuration different from that of the first embodiment will be mainly described. In the second embodiment, the diluting device 10 is omitted from the first embodiment. That is, the amount of cations supplied to the decationizing ion device 3 can be suppressed only by reducing the flow rate of the water to be treated. In this case, the flow rate of the decationized ionized water supplied to the conductivity meter 4 also decreases. When the flow rate decreases, it is desirable to confirm whether or not there is a drift in the decationization ion device 3. It is desirable that the flow rate is equal to or higher than the minimum permissible flow rate of the conductivity meter 4, and if it is less than the minimum permissible flow rate, it is desirable to change the conductivity meter 4 to a minute flow rate type. In the present embodiment, the valve 7 is used to reduce the flow rate, but any flow path resistance member can be used as long as the object is achieved. That is, the flow path resistance member is not limited as long as the pressure resistance is larger than the upstream and downstream sides of the flow path resistance member, and the flow path cross section is narrowed from the upstream and downstream sides of the orifice, for example, an orifice. It may be an

(Third Embodiment)
FIG. 3 shows a conceptual diagram of a conductivity measuring system 201 (hereinafter referred to as system 201) for decationized ionized water according to a second embodiment of the present invention. In the following description, a configuration different from that of the first embodiment will be mainly described. The configuration in which the description is omitted is the same as that in the first embodiment. A heating means 15 for heating the water to be treated is provided on the pipe 6. The configuration of the heating means 15 is not particularly limited, and a heat exchanger, a ribbon heater, or the like can be used. The temperature of the condensate is usually about 40 ° C., but it drops to 20 to 30 ° C. at the installation position of the conductivity meter 4. The heating means 15 heats the water to be treated to about 50 ° C. This improves the current efficiency of the decationizing ion device 3. This is because the change in molar conductivity is larger for Na ^{+ ions and Cl − ions than for H +} ions and OH ⁻ ions, and the higher the temperature, the easier it is for ^{Na + ions to move.} However, in order to prevent deterioration of the cation exchange membranes 34 and 35 and the cation exchanger 39 of the decationizer 3, it is not preferable to supply water to be treated at a temperature higher than 50 ° C. to the decationizer 3. Therefore, it is desirable to heat the water to be treated in the range of 40 to 50 ° C. Since the heating means 15 is for improving the current efficiency of the decationizing ion device 3, the decationizing ion device 3 of the present embodiment is limited to EDI or ED.

The third embodiment can also be combined with the first and second embodiments. For example, in the first embodiment, the heating means 15 of the third embodiment can be provided between the confluence of the pipe 6 with the diluted water supply line 11 and the inlet of the decationizing ion device 3. In the second embodiment, the heating means 15 of the third embodiment can be provided between the valve 7 of the pipe 6 and the inlet of the decationizing ion device 3.

(Example)
The simulated water simulating seawater was supplied to the conductivity measurement system of the decationized ionized water of the first to third embodiments, and the seawater leakage detection ability during the steady operation of the power plant was confirmed. EDI was used as the decationizing ion device 3, a mesh plate made of SUS304 was used for the negative electrode 37, and a titanium mesh plate coated with platinum was used for the positive electrode 36. For the cation exchange membranes 34 and 35, a strongly acidic cation exchange membrane (Neocepta CMX (manufactured by Tokuyama Soda Co., Ltd.)) in which a sulfonic acid group was introduced into a styrene-divinylbenzene copolymer base was used. The desalting chamber 31 was filled with a monolith. The ion exchange capacity of the monolith was 4.0 mg equivalent / g in terms of dry porous body, and it was confirmed by mapping sulfur atoms using EPMA that the sulfonic acid group was uniformly introduced into the porous body. .. Further, as a result of SEM observation, the internal structure of this porous body has an open cell structure, most of the macropores having an average diameter of 30 μm overlap, and the average diameter of the mesopores formed by the overlap of the macropores and the macropores. The value was 5 μm and the total pore volume was 10.1 ml / g. Foxborough's 875CR (monitor) and 871CC (sensor) were used as the conductivity meter 4.

As the simulated water (water to be treated), ammonia water in which ammonia was dissolved in pure water having a specific resistance of 18.2 MΩ · cm (conductivity: 0.054 μS / cm) was used. Sodium chloride was further added to this ammonia water to simulate seawater leakage. The flow rate of the water to be treated was 50 l / h, the direct current applied between the positive electrode 36 and the negative electrode 37 was 1.0 A, and the voltage was 40 V.

(Comparative Example) In the simulated water having an ammonia concentration of 2.0 mg / L (pH 10.0), the conductivity of the outlet water of the decationizing device 3 is 0.06 μs / cm, and the ammonia concentration is 3.6 mg / L (pH 10). In the simulated water of 3.3), the conductivity of the outlet water of the decationizing device 3 was 0.095 μS / cm and ammonia was 5 μg / L. From this, it was found that some ammonia could not be removed.

(Example 1: Corresponding to the first embodiment) Ammonia water with pH 10.3 was prepared by adding aqueous ammonia to pure water, and 0.5 mg / L of NaCl (Example 1-1) and 1 mg of NaCl were added thereto. / L (Example 1-2) was added to prepare simulated water. The simulated water having a pH of 10.3 and pure water are mixed at a volume ratio of 1: 4 to prepare simulated water having a pH of 9.7 (5-fold diluted water), and the decationizing ion device 3 is used to perform decationizing treatment. The conductivity of water was measured.

The electrical conductivity of Example 1-1 (diluted NaCl concentration 0.1 mg / L) was 1.2 μS / cm, and that of Example 1-2 (diluted NaCl concentration 0.2 mg / L) was 2. It was 4 μS / cm. This corresponds to the theoretical value of electrical conductivity when Cl becomes hydrochloric acid. From this, it was found that seawater leakage can be detected.

(Example 2: Corresponding to the second embodiment) The pH of the ammonia water was changed from 10.0 (ammonia concentration 2.0 mg / L) of Comparative Example to 10.3 (ammonia concentration 3.6 mg / L). Simulated water was prepared by adding 0.5 mg / L (Example 2-1) and 1 mg / L (Example 2-2) of NaCl to this ammonia water. The flow rate of the simulated water supplied to the decationization ion device 3 and the conductivity meter 4 was halved from that of the comparative example. In Example 2-1 (NaCl concentration 0.5 mg / L), the electric conductivity was 3.6 μS / cm, and in Example 2-2 (NaCl concentration 1 mg / L), the electric conductivity was 7.2 μS / cm. .. This corresponds to the theoretical value of electrical conductivity when Cl becomes hydrochloric acid. From this, it was found that seawater leakage can be detected.

(Example 3: Corresponding to the third embodiment) The pH of the ammonia water was changed from 10.0 (ammonia concentration 2.0 mg / L) of Comparative Example to 10.3 (ammonia concentration 3.6 mg / L). Simulated water was prepared by adding 0.5 mg / L (Example 3-1) and 1 mg / L (Example 3-2) of NaCl to this ammonia water. The simulated water was heated to 50 ° C. and supplied to the decationization ion device 3. In Example 3-1 (NaCl concentration 0.5 mg / L), the electric conductivity was 3.6 μS / cm, and in Example 2-3 (NaCl concentration 1 mg / L), the electric conductivity was 7.2 μS / cm. .. This corresponds to the theoretical value of electrical conductivity when Cl becomes hydrochloric acid. From this, it was found that seawater leakage can be detected.

1,101,201 Conductivity measurement system 2 Flow meter 3 Decationing ion device 4 Conductivity meter 6 Piping 7 Valve 8 Condenser piping 10 Diluting device 15 Heating means 31 Desalting chamber 32, 33 Concentration chamber 38 Power supply 39 Cationic exchange body

Claims (11)

To produce diluted water to be treated with a lowered pH by adding diluted water to the water to be treated containing cations and anions.
To generate decationized water by supplying the diluted water to be treated to the decationized ion device,
A method for measuring the conductivity of decationized water, which comprises supplying the decationized water generated by the decationization device to a conductivity meter and measuring the conductivity of the decationized water. The method for measuring the conductivity of decationized water according to claim 1, wherein the pH of the water to be treated is 10 or more. The method for measuring the conductivity of decationized water according to claim 1 or 2, wherein the diluted water is decationized water previously generated by the decationization device. The method for measuring the conductivity of decationized water according to any one of claims 1 to 3, wherein the decationized ion device is an electroregenerative decationized ion device or an electrodialysis device. The dilution and a child warming prior to feeding to the decationizing device water to be treated, method of measuring the conductivity of decationized water according to claim 4. The method for measuring the conductivity of decationized water according to any one of claims 1 to 5, wherein the water to be treated is condensate from a thermal power plant or a nuclear power plant. A diluting device that adds diluted water to the water to be treated containing cations and anions to generate diluted water to be treated with a lowered pH.
A decationizing ion device that generates decationized ionized water from the diluted water to be treated, and
A system for measuring the conductivity of decationized water, which comprises a conductivity meter for measuring the conductivity of decationized water generated by the decationized ion device. The diluting device includes a container for storing decationized water generated by the decationization device and passing through the conductivity meter, a water supply line connecting the container to the inlet of the decationization device, and the water. The system for measuring the conductivity of decationized water according to claim 7, further comprising a transfer pump provided on the supply line. The system for measuring the conductivity of decationized water according to claim 7 or 8, wherein the decationization device is an electroregenerative decationization device or an electrodialysis device. It said to have a heating means for heating before supplying dilution water to be treated the decationizing device, the measurement system of the conductivity of decationized water according to claim 9. The system for measuring the conductivity of decationized water according to any one of claims 7 to 10, wherein the water to be treated is condensate from a thermal power plant.

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