JPH10174890A - Treatment of ammonia type condensate desalting device and water passage tower using to this - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a treatment method and a water passage tower using to this enabling to lower a quantity of impurities such as Na in the treated water by an ammonia type condensate desalting device. SOLUTION: In this treating method, condensate is passed through the water passage tower of the condensate desalting device filled of ion-exchange resin composed of cation exchange resin mixed with anion exchange resin, and an ammonia type condensate treatment is performed. In this case, water passage of the water passage tower is interrupted, and aqueous ammonia is flown and the impurities in the mixed ion-exchange resin are removed outside the water passage tower, and then the condensate is again made to flow.

Description

DETAILED DESCRIPTION OF THE INVENTION

[0001]

BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method of treating condensate in an ammonia type condensate desalination apparatus for treating condensate in a thermal power plant or a nuclear power plant. The present invention relates to a method for preventing an increase in impurities by a simple operation and a water tower used for the method.

[0002]

2. Description of the Related Art Conventionally, in the treatment of condensate in a thermal power plant or the like, the condensate is treated with a mixed resin of an NH ₄ type strongly acidic cation exchange resin and an OH type strongly basic anion exchange resin, so-called ammonia. A type condensate desalination unit is used. The ammonia-type condensate desalination apparatus removes other impurities in the condensate water without removing a large amount of ammonium ions present in the condensate water. The chemical cost is lower than that of a so-called hydrogen type condensate desalination apparatus using a mixed resin of an ion exchange resin and an OH type strongly basic anion exchange resin.
The ammonia type condensate desalination apparatus includes a plurality of water towers for treating condensate, a regeneration facility for regenerating the mixed resin used in the water tower, and storing the regenerated mixed resin, It consists of a water tower and a resin transfer pipe for taking the mixed resin in and out of the regeneration equipment.

A conventional ammonia-type condensate desalination apparatus uses a strongly mixed cation exchange resin (hereinafter referred to as a cation exchange resin) in a regeneration facility.
Is regenerated to H-type, and strongly basic anion exchange resin (hereinafter referred to as anion exchange resin) is regenerated to OH-type, and a mixed resin of both H-type and OH-type ion-exchange resins is filled into a water tower. The conversion of the H-type cation exchange resin into the NH ₄ type is carried out by using ammonium hydroxide injected into the condensate water to prevent corrosion of piping and the like while passing the condensate water. Therefore, even if it is an ammonia type condensate desalination device, it will be operated as a hydrogen type condensate desalination device at the initial stage of passing water, and the H-type cation exchange resin will be converted to an NH ₄ type cation exchange resin during the passage of water. It is operated as an ammonia-type condensate desalination unit from the water passed after the conversion.

However, in the ammonia type condensate desalination apparatus, ammonium ions leak into the treated water of the water flow tower, and even if the amount of the ammonium ions becomes the same as that in the condensate which is the raw water to be treated, the ammonia water is still supplied. Thus, since the sodium ions (hereinafter referred to as Na ⁺ ) and other impurities in the condensate are removed, the cation exchange resin is particularly strictly regenerated. In other words, speaking of the cation exchange function of the ammonia type condensate desalination apparatus, the NH ₄ type cation exchange resin ion-exchanges a small amount of Na ⁺ in condensate in which ammonium ions are present in a large amount. If the cation exchange resin contains more than a specified amount of Na-type cation exchange resin, ammonium ions leak into the treated water of the water flow tower almost simultaneously with Na ⁺ leakage. Exceed it. Therefore, in order to operate the ammonia-type condensate desalination apparatus without any problem without such a condition, the above-mentioned specified value is defined as the sodium fraction of the cation exchange resin after regeneration (the molar ratio of the Na-type exchange group to the total exchange groups) (Fraction) must be 0.003 or less.

[0005] The reason that the Na-type cation exchange resin is mixed into the mixed resin after regeneration is that the amount of acid used to convert the used cation exchange resin into H-type satisfies the required amount. In the following points. That is, the sodium hydroxide solution used when regenerating the anion exchange resin comes into contact with the cation exchange resin, and the cation exchange resin that has become Na type due to this contact is directly mixed into the mixed resin after regeneration. One of the mixing routes is a case where both ion exchange resins are separated by back washing and, for example, the upper anion exchange resin and the lower cation exchange resin separated into two layers are regenerated as they are (1). When the recovery waste liquid of the anion exchange resin is taken out from the separation boundary with a collector, the point is that the regeneration waste liquid containing a large amount of sodium hydroxide comes into contact with the cation exchange resin. After separating both ion-exchange resins, the upper layer anion-exchange resin is transferred to another column, and both ion-exchange resins are regenerated in separate columns (two-column regeneration). The point is that a small amount of a cation exchange resin existing on the separation interface is mixed, and a sodium hydroxide solution as a regenerant comes into contact with the cation exchange resin. Another mixing route is that a fine cation exchange resin that cannot be backwashed and separated by a water flow is mixed into the anion exchange resin, and the sodium hydroxide solution comes into contact with the cation exchange resin.

[0006] To solve these problems, for example, 1
In tower regeneration, by setting the installation position of the collector in the anion exchange resin layer above the separation boundary,
A method to prevent the wastewater containing sodium hydroxide from coming into contact with the cation exchange resin near the separation boundary. In the case of two-column regeneration, the upper layer anion exchange resin is transferred to another column after backwashing and separation. In such a case, there is a method in which a small amount of anion exchange resin is left and transferred above the separation interface to prevent the cation exchange resin near the interface from being mixed into another column. In the two-column regeneration, a small amount of anion exchange resin in the upper layer of the separation boundary and a small amount of anion exchange resin below the separation boundary are further transferred to another column.
There is a method in which the transferred mixed resin is stored without regeneration, combined with the mixed resin sent next time, and then transferred to another tower as a resin that is not always regenerated in the same manner as described above. By adopting, the regenerant of the cation exchange resin is also prevented from coming into contact with the anion exchange resin. As a countermeasure against the fine cation exchange resin present in the anion exchange resin, after regenerating the anion exchange resin, the ammonium hydroxide solution is passed through and the fine cations present in the anion exchange resin are removed. When the exchange resin is converted from Na type to NH ₄ type, or when the mixed resin is separated, specific gravity separation is performed using a concentrated sodium hydroxide solution having an intermediate specific gravity between both ion exchange resins, instead of backwashing separation using a water flow. The method is adopted. However, the method using an ammonium hydroxide solution is becoming a less preferable method today in which excess ammonium ions are discharged out of the system as a regeneration waste liquid, and the nitrogen regulation of the wastewater is becoming stricter. With the increase in initial cost, a large amount of cation exchange resin is completely converted into Na type at the time of specific gravity separation, and when this is regenerated into H type, the amount of acid used must be considerably larger than before, and running This results in increased costs and is also an undesirable method. Therefore, in the recent ammonia-type condensate demineralizer, the ion exchange resin, particularly the cation exchange resin, which is initially charged into the apparatus, shall be as fine as possible, excluding the fine cation exchange resin. The two-tower regeneration described above is employed.

[0007]

However, such an ammonia type condensate desalination apparatus, even if a fine cation exchange resin is removed as much as possible as the cation exchange resin to be initially charged, is used. However, the flow rate of the condensate in the water tower is quite high and the pressure loss is large, or the flow of water, transfer, regeneration and transfer is repeated. Ion exchange resin increases. Therefore, as this increase progresses, the above-mentioned sodium content cannot be reduced to 0.003 or less, and the mixed resin of the H-type cation exchange resin and the OH-type anion exchange resin transferred from the regeneration equipment is passed through the water tower. And used as a hydrogen-type condensate desalination unit at the beginning of the water flow, and an ammonia-type condensate desalination unit after the point when the H-type cation exchange resin was converted to an NH ₄ type cation exchange resin. In this case, the leakage amount of sodium ions increases at the same time as the ammonium ions leak into the treated water, and the leakage amount of the sodium ions exceeds the allowable value,
There is a problem that it cannot be operated as an ammonia type condensate desalination apparatus.

In the case of such a two-tower type regeneration method,
There are problems such as complicated reproduction equipment and complicated reproduction operation.

Further, after the condensing demineralization tower shifts from the H-type cation exchange resin to the NH ₄ type cation exchange resin, or after the NH ₄ cation exchange resin flows, the seawater leaks in the condenser. Occurs, R-Na, R-C
l, and impurities such as R-SO ₄ is gathered around the lower portion of the ion exchange resin was transferred to an ion-exchange resin in this state to the reproduction equipment, Na with concentrated aqueous ammonia ^+, Cl ^- and SO ₄
Attempts have been made to eliminate ^{2- and} other ions out of the system,
Disturbance occurs in the ion exchange zone at the stage of transfer to the regeneration facility, and a large amount of aqueous ammonia is required to eliminate these ions. In this case, the wastewater of the ammonia water is directly diluted and discharged into the sea area or treated together with the wastewater generated from the entire power generation plant by the nitrogen removal equipment, but in the former case, from the viewpoint of reducing the environmental burden in the future The equipment needs to be improved, and in the latter case, there is a problem that the treatment equipment becomes excessively large because the wastewater including the wastewater generated from various places is removed.

Therefore, an object of the present invention is to prevent an increase in impurity ions such as sodium ions in the treated water at the time of shifting from the hydrogen type condensate desalination treatment to the ammonia type condensate desalination treatment by a simple operation. To provide a method for treating an ammonia-type condensate desalination apparatus.

It is another object of the present invention to provide a method for treating an ammonia-type condensate desalination apparatus capable of reducing the burden on the environment without discharging nitrogen-containing wastewater.

[0012]

Under such circumstances, the present inventors have made intensive studies and as a result, when the water-flow tower shifts from H-type cation exchange resin to NH ₄ -type cation exchange resin operation, Na ⁺ , Cl ^- and against phenomena leakage amount increases the impurity ions SO ₄ ^2-like, interrupting the water flow of the water passing tower, kept in a state that does not disturb the ion exchange zone in the interior of the ion exchange resin, separately, ammonia water was injected from the top, Na ion exchange resin be blown from the bottom ^+, Cl ^- and sO ₄ that impurities ² etc. can be effectively eliminated Togai, also interrupt the vent water The operation of injecting ammonia water is effective even when the impurity ions trapped in the ion-exchange resin due to leakage of seawater or the like start to leak from the tower outlet in NH ₄ type water flow, Ammoni Water may be be purified and reused without discarding, according to this, found such that can achieve the above object, and have completed the present invention.

That is, the present invention relates to a method for carrying out ammonia-type condensate treatment by passing condensate water through a water tower of a condensate desalination apparatus filled with an ion exchange resin obtained by mixing a cation exchange resin and an anion exchange resin. The condensate flow in the water tower is interrupted, the ammonia water is passed through the water tower where the water flow has been interrupted, impurities in the mixed ion exchange resin are removed outside the water tower, and then the condensate water is passed. A method for treating an ammonia-type condensate desalination apparatus characterized by resuming water and the ammonia wastewater blown from the lower part of a water tower when the ammonia water is passed is purified by distillation or a degassing membrane and reused. An object of the present invention is to provide a method for treating an ammonia type condensate desalination apparatus.

According to the present invention, there is further provided a mixed ion-exchange resin filled portion of a cation-exchange resin and an anion-exchange resin therein, a condensate inflow pipe and an ammonia water inflow pipe disposed at an upper part, and a sodium monitor detection at a lower part. An object of the present invention is to provide a water tower provided with a liquid discharge pipe, a condensate outflow pipe, and an ammonia water blow pipe.

[0015]

DESCRIPTION OF THE PREFERRED EMBODIMENTS In the present invention, the type, mixing ratio, filling amount and the like of a mixed ion exchange resin of a cation exchange resin and an anion exchange resin to be filled in a water tower of a condensate desalination apparatus are known. Can be applied.

In the present invention, the condensate treatment is a condensate treatment using an ammonia type condensate desalination apparatus such as a PWR type nuclear power plant or a thermal power plant. The condensed steam is cooled to form condensate water, and the condensate is heated and again converted to steam as Na ⁺ and Cl ⁻ contained in the condensate of the circulation system that drives the power generation turbine.
And a process for removing various impurity ions such as SO ₄ ^2- and cladding.

In the present invention, the timing for interrupting the flow of water may be a transition from the hydrogen-type condensate desalination to the ammonia-type condensate desalination, or almost immediately before the transition, or after the ammonia-type condensate desalination. It is preferable that sodium ions start to leak from the outlet of the water tower, especially when the sodium ion is discharged from the outlet of the water tower after the transition from the hydrogen type condensate desalination process to the ammonia type condensate desalination process and after the ammonia type condensate desalination process. Is preferred because ammonia water can be produced in a minimum necessary amount.

[0018] The above and the time of transition of the hydrogen-type condensate demineralizer process from (hereinafter referred to H-treated) ammonium type condensate demineralizer process to (hereinafter referred to as NH ₄ form process), the water flow tower outlet of condensate treated water In the typical example of the temporal transition as shown in FIG. 1 obtained by monitoring, the initial time point of the transition period from the H-type treatment to the NH ₄ -type treatment indicated by the point S immediately before the increase in the amount of sodium ion leakage. Say. During this transition, if the flow of water is interrupted and ammonia water is injected into the water flow tower, the Na ⁺ , Cl ⁻ and SO ₄ ² held in the mixed resin filled with the required minimum amount of ammonia water can be obtained. ^-
Impurities can be effectively eliminated.

In addition, almost immediately before the transition of the cation exchange resin from the H-type treatment to the NH ₄ -type treatment, the cation exchange resin is in the H-type treatment state, and NH ₄ generated after that is in the state.
Since the shift to the mold treatment, that is, the leak of the impurities is performed in anticipation, it is not necessary to use a large amount of ammonia water just before the shift from the H-type treatment to the NH ₄ -type treatment. preferable.

In the present invention, even if Na ⁺ is detected from the outlet of the water tower due to seawater leak or the like in the condenser after shifting to the NH ₄ type treatment, the water flow is interrupted.
Ammonia water is passed through the water tower to remove impurities, but a sodium monitor is installed at the water tower inlet, and when a predetermined amount or more of Na ⁺ is detected, the ammonia water may be injected. . Also, when the water flow in the water tower is interrupted and the ammonia water is passed, the impurity ions are concentrated in the ion exchange resin at the lower part of the water tower,
In order to desorb this efficiently, it is preferable to pass the ammonia water from the upper part of the water tower without disturbing the ion exchange resin particularly at the lower part of the water tower.

As the ammonia concentration of the ammonia water,
If the content is 1.0% or more, the impurities can be effectively eliminated, but usually 2 to 4% is preferable.

The ammonia wastewater blown from the lower portion of the water tower may be transferred to a wastewater treatment facility as it is. However, after purification by distillation or a degassing membrane, it is necessary to reuse the wastewater containing nitrogen. This is preferable from the viewpoint of reducing environmental load and saving resources. The purification method using the distillation or degassing membrane is not particularly limited, and a known method can be used.

As a water tower used in the method for treating an ammonia type condensate desalination apparatus of the present invention, for example, a water tower 50 as shown in FIG. 2 can be mentioned. The water flow tower 50 is filled with a mixed ion exchange resin 7 of a cation exchange resin and an anion exchange resin, a water collecting collector 9 is provided below the filled portion, and a condensate flow meter is provided at an upper portion. 12 and a condensate inlet pipe 1 having a condensate distributor 8 at its end, an ammonia water inlet pipe 2 having an ammonia water inlet valve 23, and a manhole 3; Sodium detection liquid discharge pipe 6 having a sodium monitor inlet valve 26 and a sodium monitor 11, a sample collection pipe 31 having a sample collection valve 27, a condensate outflow pipe 4 having a condensate outlet valve 22, and ammonia water blow Ammonia water blow pipes 5 each having a valve 24 are provided.

The ammonia water inflow pipe 2 has an ammonia dilution water flow meter 13 and a pure water transfer pipe 32 having a pure water inlet valve 28 on the upstream side, and an ammonia flow meter 14 and an ammonia water inlet which are guided by the chemical ejector 10. Valve 29
Into the ammonia stock solution inflow pipe 33 having Also,
The condensate inflow pipe 1 is provided with a flush water inflow pipe 34 having a flush water valve 25 that bypasses the condensate inlet valve 21.

Next, an apparatus and a flow for purifying and reusing ammonia water will be described with reference to FIG. In FIG. 3, the same components as those in FIG. As shown in FIG. 3, a drainage tank 35 in which an ammonia water blow pipe 5 is disposed on the upstream side, a deaeration film 36, a cooling absorption tower 37, and an ammonia storage tank 3 on the downstream side, respectively.
8, a heating tank 39, a distillation tower 40, an ammonia absorption tower 41, and an ammonia recovery tank 42 in which a return transfer pipe 48 to the ammonia stock solution inflow pipe 33 is disposed downstream, and these are connected by connection pipes, respectively. . Although not shown, it goes without saying that the ammonia-type condensate desalination apparatus of the present invention is provided with the above-mentioned regeneration equipment and resin transfer pipe in addition to the water tower.

The operation procedure of the water tower in the ammonia type condensate desalination apparatus of the present invention is as follows. In FIG.
The condensate inlet valve 21 and the condensate outlet valve 22 are opened in the water flow tower 50, and a part of the condensate of the power plant is passed. Also, the sodium monitor 11 is operated. The condensate flow rate is monitored by the condensate flow meter 12. From the predetermined water supply time or the total amount of condensate water condensed, the transition from the H-type treatment to the NH ₄ type treatment or almost immediately before the transition, or the sodium detection value detected by the sodium monitor 11 reaches the predetermined value. Then, perform the following operation. That is, the condensate inlet valve 21 and the condensate outlet valve 22 are closed to interrupt the flow of the condensate water to the water tower, and the ammonia water is passed to the water tower where the water flow was interrupted. At this time, since impurities such as sodium ions are concentrated in the ion exchange resin at the lower part of the water tower, water flow was interrupted without disturbing the ion exchange resin layer by backwashing or air mixing. Ammonia water is passed in the state as it is.

First, the ammonia water inlet valve 23, the ammonia water blow valve 24, and the pure water inlet valve 28 are opened to flow pure water to drive the drug ejector 10, and then the ammonia water inlet valve 29 Is opened to allow high-concentration (for example, 25% ammonia water) ammonia to be sucked. The pure water flow rate is monitored by an ammonia dilution water flow meter 13,
It is adjusted by the pure water inlet valve 28. The flow rate of the ammonia water is monitored by the ammonia flow meter 14, and the ammonia water inlet valve 2
Adjust with 9. The passage of the ammonia water is stopped when the Na ⁺ in the ammonia drainage falls below a predetermined value by monitoring the sodium monitor 11 at the outlet of the water tower, and the ammonia water inlet valve 23, the ammonia water blow valve 24, the pure water inlet The valve 28 and the ammonia water inlet valve 29 are closed.

Next, cleaning is performed to discharge the ammonia water out of the system. That is, the flush water valve 25 and the condensate blow valve 51 may be opened, and the flush water amount is monitored by the condensate flow meter 12 and adjusted by the flush water valve 25. The washing time is determined by the capacity of the water tower and the amount of water flow, but it is preferable to wash for a slightly longer time than this without leaving ammonia water. The washing is completed by closing the washing water valve 25 and the condensate blow valve 51. The condensed water collected after the condensed blow valve 51 is collected through a pure water device not shown.

Next, a condensate inlet valve 21 and a condensate outlet valve 22
And restart the condensate flow. The flow rate of the passing water is monitored by the condensate flow meter 12. After the condensate water flow is resumed, the water tower continues to flow until the end of the ammonia type treatment, and then the ion exchange resin in the water tower is transferred to the regeneration facility by resin transfer pipes and processed in a usual manner. Will be played.

The Na ⁺ concentration in the treated water at the outlet of the water tower is monitored by opening the sodium monitor inlet valve, and the Cl ⁻ and SO ₄ ²⁻ concentrations are obtained by opening the sampling valve 27 and collecting and analyzing the sample water. Desired. The vent valve 30 is used when filling the water tower with the ion exchange resin and then extracting air accumulated in the water tower, and the manhole 3 is used when inspecting the inside of the water tower and filling the ion exchange resin. .

The operating procedure for purifying and reusing ammonia water is as follows. That is, in FIG.
When the ammonia water flows, the drain water from the water tower 50 is drained into the drain tank 3.
After being stored in 5, ammonia is recovered. That is, the drainage containing ammonia at about 30 ° C. stored in the drainage tank 35 is passed through the deaeration membrane 36 by the pump 44. The passage side of the deaeration membrane 36 is connected to a cooling absorption tower 37, which is cooled by cooling water of about 20 ° C. and is evacuated by a vacuum pump 45 to about 9.8 × 10 ⁴ Pa. The ammonia gas that has passed through the degassing film 36 is cooled inside the cooling absorption tower 37, and increases the absorption rate of the pure water to be sprayed. Next, the ammonia absorbed in the pure water is stored in the ammonia storage tank 38. In addition, the ammonia gas not absorbed by the cooling absorption tower 37 is guided to an ejector 43 provided on a circulation line of the degassing film 36 to the drainage tank 35 for ejecting water, and returned to the drainage tank 35. The above processing is completed when the concentration of ammonia in the drainage tank 35 becomes low, and the wastewater in the ammonia storage tank 38 is sent to the heating tank 39 to perform a separate drainage treatment. That is, if the Na concentration of the ammonia water stored in the ammonia storage tank 38 is 2.5 mg / l or less, the ammonia water is transferred to the ammonia recovery tank 42 and sent to the ammonia stock solution transfer pipe 33 by the pump 47 for reuse. . If the Na concentration of the ammonia water exceeds 2.5 mg / l, the ammonia water is supplied to the heating tank 39, the distillation column 40 and the ammonia absorption column 4
After passing through 1, the concentration of Na is reduced to 2.5 mg / l or less, and collected and reused in the ammonia recovery tank 42 in the same manner as described above. The ammonia concentration in the ammonia recovery tank 42 was 25%.
When the amount is less than the above, the operation may be performed by increasing the amount of ammonia and decreasing the amount of ammonia dilution water.

[0032]

According to the processing method of the ammonia type condensate desalination apparatus of the present invention, it is possible to minimize the leakage of impurities such as Na ⁺ when the cation exchange resin is changed from H type to NH ₄ type. And scale adhesion to the turbine can be prevented. Further, since the blown ammonia water is purified and reused, the burden on the environment can be reduced without discharging the nitrogen-containing wastewater. For this reason, the water quality standard of the supply water to the steam generator is strict (Na ⁺ is 0.06 μg / l or less, Cl ⁻ is 0.15 μg / l or less).
The ammonia type condensate desalination process can be used even in the condensate desalination device installed in the PWR type power plant where only the mold process operation was performed, and the cost can be reduced.

[0033]

Next, the present invention will be described in detail with reference to examples, but this is merely an example and does not limit the present invention.

Example 1 (Elimination of impurities at the time of transfer from H-type to NH ₄ -type cation exchange resin) The ion composition of the ion-exchange resin used in the test was actually changed from H-type to NH ₄ -type treatment. Considering the ion composition used in the normal condensate desalination tower at the time of transfer, it was as shown in Run 1 in Table 1. The ion-exchange resin was charged into the water-flow tower from the water-flow tower resin inlet at a volume ratio of the anion-exchange resin 1 to the cation-exchange resin 2 so that the resin after filling could be kept in a sufficiently mixed state. Also,
In order to prevent the ion exchange resin from being separated at the time of filling, the water level in the water flow tower at the time of filling is higher than the ion exchange resin layer by 50.
Filling was performed while replenishing pure water so as to keep mm. After filling the ion-exchange resin, the resin inlet was closed, the vent valve was opened, the water tower was filled with water, the vent valve was closed, and the system was washed with pure water (ammonia diluted water) for 1 hour and then transferred to test water flow. The used water tower and test conditions are shown below, and the operation method was the same as the operation procedure of the water tower of the ammonia type condensate desalination apparatus described above. FIG. 4 shows the results of ion exclusion of Na ⁺ , Cl ⁻ and SO ₄ ²⁻ after passing through the aqueous ammonia.

(Water Tower) The water tower shown in FIG. 2 was used. Cation exchange resin: Amberlite 200 cT Filling amount 400 liter (based on Na type) Anion exchange resin: Amberlite 1RA900 Filling amount 200 liter (based on Cl type)

(Test conditions) Condensed water quality: NH ₃ 2000 μg / l, N ₂ H ₄ 300 μg / l Pure water: conductivity 0.1 μS / cm or less Ammonia stock solution concentration: 25% Aqueous ammonia flow solution concentration: 4% Ammonia Water flow time: 1.5 hours Cleaning flow rate: 13 m ³ / H Cleaning time: 1 hour Water flow rate: 60 m ³ / H

Example 2 (Elimination of Impurities Associated with Seawater Leak after Transfer to NH ₄ Type Water) The ion composition of the ion exchange resin used in the test was as follows:
The same method as in Example 1 was followed except that the seawater leak of about 50 μg CaCO ₃ / l continued for 3 hours during the NH ₄ type water flow, as shown in Run 2 of Table 1. The results are shown in FIG.

[0038]

[Table 1]

From FIGS. 4 and 5, it was confirmed that most of the ions adsorbed on the ion exchange resin were removed in the ammonia water flow, and almost all the ions were removed at the end of the washing. In the water-passing treatment restarted after the ammonia water was passed through the water-passage tower, each ion concentration of the treated water in the water-passage tower was 0.016 to 0.018 as Na ⁺ .
μg / l, Cl ^- at 0.13~0.14μg / l, SO ₄ ^2-
0.12 to 0.13, and the strictest treatment water quality standard such as PWR (Ni ⁺ : 0.06 μg / l or less, Cl
^- : 0.15 μg / l or less), demonstrating that the present invention is applicable not only to thermal power plants but also to PWRs.

[Brief description of the drawings]

FIG. 1 is a diagram showing the results of measuring the change over time of treated water quality which appears during operation in a normal state in an ammonia type condensate desalination apparatus.

FIG. 2 is a flowchart showing an example of an embodiment of a water tower according to the present invention.

FIG. 3 is a flowchart showing an example of an embodiment of an ammonia type condensate desalination apparatus of the present invention.

FIG. 4 is a diagram showing a relationship between impurities of treated water and a water passage time in Run 1 of the embodiment of the present invention.

FIG. 5 is a diagram showing a relationship between impurities of treated water and a water passage time in Run 2 of the embodiment of the present invention.

[Explanation of symbols]

 DESCRIPTION OF SYMBOLS 1 Condensate inflow pipe 2 Ammonia water inflow pipe 4 Condensate outflow pipe 5 Ammonia water blow pipe 6 Sodium monitor detection liquid discharge pipe 7 Mixed ion exchange resin filling part 8 Water flow distributor 9 Water collecting collector 10 Drug discharge ejector 11 Sodium monitor 12 Water Water flow meter 13 Ammonia dilution water flow meter 14 Ammonia flow meter 21 Condensate inlet valve 22 Condensate outlet valve 23 Ammonia water inlet valve 24 Ammonia water blow valve 25 Wash water valve 26 Sodium monitor inlet valve 27 Sample collection valve 28 Pure water inlet Valve 29 Ammonia water inlet valve 30 Vent valve 31 Sampling pipe 32 Pure water transfer pipe 33 Ammonia stock solution inflow pipe 34 Washing water inflow pipe 35 Drain tank 36 Deaeration membrane 37 Cooling absorption tower 38 Ammonia storage tank 39 Heating tank 40 Distillation tower 41 Ammonia absorption Tower 42 ann Near the collecting tank 43 the ejector 44, 45, 46, 47 pump 50 water communicating column 51 condensate blow valve

Claims (4)

[Claims] 1. A method of performing an ammonia type condensate treatment by passing condensate water through a water tower of a condensate desalination apparatus filled with an ion exchange resin in which a cation exchange resin and an anion exchange resin are mixed. The flow of water is interrupted, the ammonia water is passed through the water tower where the water flow was interrupted, impurities in the mixed ion exchange resin are eliminated outside the water tower, and then the flow of condensate water is resumed. A method for treating an ammonia-type condensate desalination apparatus, comprising: 2. A time when the flow of water is interrupted is when the water type condensate desalination process is shifted to the ammonia type condensate desalination process, almost immediately before the shift, or after the ammonia type condensate desalination process. 2. The method for treating an ammonia type condensate and desalination apparatus according to claim 1, wherein sodium ion starts to leak from the outlet. 3. The ammonia-type condensate according to claim 1, wherein the ammonia wastewater blown from the lower portion of the water tower when the ammonia water is passed is purified by distillation or a degassing membrane and reused. Processing method of desalination equipment. 4. A mixed ion-exchange resin filled portion of a cation-exchange resin and an anion-exchange resin therein, a condensate inflow pipe and an ammonia water inflow pipe disposed in an upper part, and a sodium monitor liquid discharge pipe in a lower part. A water tower provided with a condensate outflow pipe and an ammonia water blow pipe.