JP2012152690A - Condensate treatment method, and condensate treatment apparatus - Google Patents

Abstract

PROBLEM TO BE SOLVED: To provide a condensate treatment method and a condensate treatment apparatus by which organic acids can be sufficiently removed without using a desalting tower of a mixed bed system.SOLUTION: In the condensate treatment method where at least a part of boiler condensate is treated by an ion exchange resin and then is supplied to the boiler, the ion exchange resin is consisting of an anion exchange resin. Since the organic acids in the boiler condensate is removed by the anion exchange resin, the organic acids can be removed without installation of the desalting tower of the mixed bed system. Further when amine or the like is added to boiler water as a pH adjuster or the like, removal of even amine or the like is prevented at the time of removal treatment of the organic acids by the anion exchange resin.

Description

  The present invention relates to a condensate treatment method and a condensate treatment apparatus for treating condensate containing an organic acid.

  Ion exchange water and demineralized water are mainly used for boiler water. This boiler water is supplied to the boiler as boiler feed water to be steam, and is used for power generation by a steam turbine, and then condensed to condensate. This condensate is circulated and used as boiler feed water.

In boiler equipment equipped with these boilers, steam turbines, and the like, there is a problem that organic acids are generated in the boiler can water, and the pH is lowered to cause corrosion.
That is, the organic matter contained in the boiler water may be brought into the boiler facility and decomposed to produce an organic acid. In addition, an organic acid may be generated due to an organic oxygen scavenger added to boiler water. The organic acid that lowers the pH of boiler can water is not limited to boiler can water, but is transferred to condensate with steam and then again to boiler feed water, and is thus circulated and concentrated in the system. In particular, the organic acid is more concentrated by reducing the amount of blow intended to save energy and save water. When these organic acids lower the pH of boiler water, metals such as iron are eluted and corrosion progresses.

Since organic acids are easily concentrated in boiler can water, phosphate-based cleansing agents (mixtures of sodium phosphate and sodium hydroxide) are used as pH adjusters as a countermeasure against corrosion of boiler can bodies.
However, even if such a phosphate-based cleansing agent is used, it is still not possible to prevent a decrease in the pH of boiler can water due to organic acids brought from the boiler water or organic acids caused by the organic oxygen scavenger. In addition, when a phosphate-type cleanser with a Na / PO ₄ molar ratio of 3 or more (mixed product of sodium phosphate and sodium hydroxide) is used, phosphate hide-out phenomenon (both heat transfer surface load of the boiler) When the load is high, the phosphate concentration in the boiler water increases, and when the load decreases, the original concentration returns to the original concentration, which may adversely affect heat transfer in the boiler section. Furthermore, there is a concern about the occurrence of alkali corrosion.

Further, as another preventive measure against corrosion due to organic acid, Patent Document 1 discloses that organic acid is removed using a mixed bed type desalting tower.
That is, in a thermal power plant and a nuclear power plant, as a condensate demineralizer for reusing condensate as boiler feed water, a mixed bed type dewatering device filled with anion exchange resin and cation exchange resin in a mixed state is usually used. A plurality of salt towers are installed in parallel (paragraph 0002 of the same document). By passing the condensate in an alkaline state to the mixed bed type desalting tower, the organic acid is removed with high efficiency.

JP-A-11-47744

However, the organic acid removal method of Patent Document 1 has problems such as the need to install a mixed bed type desalting tower, and the amount of pH adjuster to be added significantly increases.
That is, the boiler equipment that is the subject of this document is a boiler equipment having a mixed-bed type desalting tower, such as a thermal power plant and a nuclear power plant. In supercritical class boilers such as these thermal power plants and nuclear power plant boilers, when the seawater, raw materials, products, etc. used in the condenser cooling water leak into the boiler water, the pH of the boiler water It drops significantly. In order to cope with such contamination contaminated with boiler water, a mixed bed type desalting tower is installed. On the other hand, in private private power generation boiler facilities below the subcritical class, seawater is not used as the cooling water for condensers in most cases, so even if the cooling water leaks into the boiler water, A significant pH drop is unlikely to occur, and no mixed bed desalting tower is installed. If a mixed-bed desalting tower is installed in such boiler facilities that are not likely to be mixed with seawater, the equipment costs are high.
Further, the mixed bed type desalting tower not only removes organic acids, but also removes pH adjusting agents such as amines and ammonia (hereinafter sometimes referred to as amines). That is, the cation exchange resin in the desalting tower removes the pH adjusting agent such as amine. For this reason, it is necessary to replenish the boiler water with the amount of amine removed by the cation exchange resin, and there is a problem that the cost of medicine is high.

  An object of the present invention is to provide a condensate treatment method and a condensate treatment apparatus capable of satisfactorily removing organic acid without using a mixed bed type desalting tower as in Patent Document 1. .

As a result of intensive studies, the present inventors have found that by treating the condensate of the boiler with an anion exchange resin, the organic acid can be removed well without installing a mixed bed type desalting tower. The present invention has been completed based on such findings.
That is, the present invention provides the following.
That is, the present invention provides the following (1) to (8).
(1) A condensate treatment method in which at least a part of the condensate of the boiler is treated with an ion exchange resin and then supplied to the boiler, wherein the ion exchange resin is made of an anion exchange resin.
(2) The condensate treatment method according to (1), wherein at least a part of the condensate is mixed with makeup water and then treated with the anion exchange resin.
(3) The condensate treatment method according to (2), wherein the makeup water is treated with a cation exchange resin and then mixed with at least a part of the condensate.
(4) The condensate treatment method according to (2), wherein the makeup water is treated with a cation exchange resin, decarboxylated, and then mixed with at least a part of the condensate.
(5) An ion exchange tower in which an ion exchange resin is accommodated, a condensate pipe for supplying the condensate of the boiler to the ion exchange tower, and a water supply pipe for supplying the treated water treated in the ion exchange tower to the boiler. A condensate treatment apparatus having the ion exchange resin comprising an anion exchange resin.
(6) The condensate treatment apparatus according to (5), further comprising a makeup water supply pipe connected to the condensate pipe.
(7) The condensate treatment apparatus according to (6), wherein a cation exchange tower in which a cation exchange resin is accommodated is provided in the middle of the makeup water supply pipe.
(8) A cation exchange tower and a decarboxylation tower in which a cation exchange resin is accommodated are provided in this order from the side far from the connection point to the water supply pipe in the middle of the makeup water supply pipe. The condensate treatment apparatus as described.

  In the present invention, the organic acid in the boiler condensate is removed with an anion exchange resin. For this reason, an organic acid can be removed without installing a mixed bed type desalting tower. Moreover, when amine etc. are added as boiler pH adjuster etc. in boiler water, it is prevented that an amine etc. are removed at the time of the removal process of the organic acid by an anion exchange resin.

It is a system diagram explaining the condensate treatment method and condensate treatment apparatus which concern on 1st Embodiment. It is a systematic diagram explaining the condensate treatment method and condensate treatment apparatus which concern on the modification of 1st Embodiment. It is a systematic diagram explaining the condensate treatment method and condensate treatment apparatus which concern on 2nd Embodiment. It is a system diagram explaining the test boiler equipment for a test of comparative example 1. It is a distribution diagram explaining the test boiler equipment for a test of comparative example 3. BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a system diagram illustrating a test test boiler facility of Example 1.

<First Embodiment>
Embodiments of the present invention will be described in detail. FIG. 1 is a system diagram for explaining a condensate treatment method and a condensate treatment apparatus according to the first embodiment.
(Condensate treatment equipment and boiler equipment)
First, the boiler equipment provided with the condensate treatment apparatus which concerns on this Embodiment is demonstrated. The outlet of the boiler 1 is connected to the inlet of the power generation turbine 2 via the pipe 11, and the outlet of the power generation turbine 2 is connected to the inlet of the anion exchange tower 3 via the pipe 12. The outlet is connected to the inlet of the boiler 1 via a pipe 13. A process heat exchanger 5 and a condensate cooling heat exchanger 8 are provided in the middle of the pipe 12. A makeup water supply pipe 14 is connected in the middle of the pipe 13. Further, the chemical tank 4 is connected to the boiler 1 side of the piping 13 from the makeup water supply piping 14 via the piping 15. A blow pipe 16 is connected to the boiler 1.

As the boiler 1, a boiler of a subcritical class or less (pressure 17 MPa or less, temperature 350 ° C. or less) such as a private private power generation boiler is preferably used.
Anion exchange resin is accommodated in the anion exchange tower 3. The anion exchange resin is not particularly limited, and known ones can be used, but preferably an OH type anion exchange resin (RNR ₃ OH) is used.
In the chemical tank 4, at least one of amine and ammonia is stored as a metal corrosion inhibitor. As the amine, volatile amines such as monoethanolamine, morpholine and methoxypropanolamine are preferably used.
The boiler equipment 20 is comprised by these apparatuses 1-4 and the piping 11-16. The anion exchange resin 3, the chemical tank 4, and the pipes 12, 13, 15 constitute a condensate treatment device 21.

(Condensate treatment method and operation method of boiler equipment)
Next, a condensate treatment method and a boiler facility operation method according to the present embodiment will be described. Condensate flowing out from the anion exchange tower 3 is mixed with makeup water. After the chemical | medical agent in the chemical | medical agent tank 4 is added with respect to this mixed water of condensate and makeup water, in order to adjust pH, it is supplied to the boiler 1 as boiler feed water.
The pH of the boiler feed water is preferably adjusted to pH 8 to 10, more preferably 8.8 to 9.7, although it depends on the operating conditions of the boiler equipment 20. When it is at least the lower limit of this range, metal hydroxides and oxides such as iron and copper serve as a protective film and reduce corrosion. When the amount is not more than the upper limit of this range, the protective film is prevented from being redissolved. Thus, although the addition amount of the chemical | medical agent for adjusting pH depends on the kind of chemical | medical agent and the operating conditions of the boiler equipment 20, it is 0.01-100 mg / l with respect to boiler feed water, Preferably it is 0.1-20 mg. / L.

In this boiler 1, steam is produced from boiler feed water. This steam is supplied to the power generation turbine 2. A part of the boiler water in the boiler 1 is blown out of the system through the blow pipe 16.
This boiler can water is preferably managed so that the concentration factor is within a predetermined range. Here, the concentration factor N can be expressed as N = 100 / B (B is a blow rate). Accordingly, the concentration factor N can be managed by controlling the blow rate B (%) of boiler can water from the blow pipe 16. Here, the blow rate B (%) is calculated by the following mathematical formula.
B (%) = W / F × 100
This enrichment is preferably 10 to 1000 times, more preferably 20 to 500 times. When it is at least the lower limit of this range, the blow rate is reduced and water saving is achieved. If it is below the upper limit of this range, corrosion and carryover due to concentration of corrosive substances are suppressed. There is no restriction | limiting in particular in a blow rate, For example, it is about 0.1 to 10%.
The blowing from the blow pipe 16 may be performed continuously, intermittently at a predetermined interval, or may be performed when the water quality of the boiler can water is deteriorated below a predetermined level. .

The steam supplied to the power generation turbine 2 is used for power generation.
The steam used in the power generation turbine 2 flows out of the power generation turbine 2 and is cooled by the process heat exchanger 5 and the condensate cooling heat exchanger 8. This condensate cooling heat exchanger 8 cools the condensate below the heat resistant temperature (for example, 60 ° C.) of the anion exchange resin in the anion exchange tower 3. Thereby, the thermal deterioration of the anion exchange resin of the anion exchange resin tower 3 is suppressed, and the lifetime of the anion exchange resin is extended.

The condensate cooled in the heat exchangers 5 and 8 is supplied to the anion exchange tower 3, and the organic acid in the condensate is removed.
That is, a part of the organic substance brought into the boiler facility 20 together with the makeup water and a part of the amine added to the boiler feed water from the chemical tank 4 are decomposed in the boiler, and organic acids such as formic acid and acetic acid are generated. Therefore, an organic acid exists in the condensate supplied to the anion exchange column 3. Since these organic acids generally exist as anions, they are removed by the anion exchange resin in the anion exchange tower 3.
The anion exchange tower 3 contains an anion exchange resin, but no cation exchange resin. For this reason, the amine added as a pH adjuster is prevented from being removed by the cation exchange resin. Thereby, the addition amount of the amine from the chemical | medical agent tank 4 is reduced significantly, and reduction of chemical | medical agent cost is aimed at.

This anion exchanged condensate is discharged from the system by blowing boiler water, etc., or supplementary water is added by the amount used in the process. It is supplied to the boiler 1. In this way, the boiler water circulates in the boiler facility 20.
This makeup water may be continuously added to the condensate, or may be added periodically after a predetermined time, and is added when the quality of the boiler feed and condensate deteriorates below a predetermined level. May be.
In this boiler facility, the condensate recovery rate is not particularly limited, but is preferably 30% or more, more preferably 50% or more. Water saving is achieved when the value is above the lower limit of this range.

  In the present embodiment, since the makeup water is added downstream of the anion exchange resin tower 3, the amount of water passing through the anion exchange resin tower 3 is reduced as compared with the case where it is added upstream, and the anion exchange resin is reduced. The load on the tower 3 is reduced.

<Modification of the first embodiment>
In the said embodiment, there is no limitation in particular in the addition location of a chemical | medical agent, You may add a chemical | medical agent in the upstream from the makeup water in the piping 13. FIG. Moreover, you may add in the upstream and downstream of the heat exchanger 5 among the piping 12, may add in the boiler 1, and may add in these two or more places.
In the above embodiment, at least one of amine and ammonia is added as a drug, but other drugs such as sodium phosphate may be added in addition to or in place of it. For example, sodium phosphate may be added so that the Na / PO ₄ molar ratio is preferably 3.0 or less. By setting it within this range, the occurrence of alkali corrosion is prevented. The Na / PO ₄ molar ratio is more preferably 2.6 to 2.8.

  As shown in FIG. 2, the makeup water supply pipe 14 may be connected in the middle of the pipe 12. In this case, the condensate from the power generation turbine 2 is cooled by make-up water and then supplied into the anion exchange resin tower 3. Thereby, even when the water temperature at the outlet of the process heat exchanger 5 is high (for example, higher than 60 ° C.), it is possible to prevent thermal deterioration of the anion exchange resin without providing the condensate cooling heat exchanger 8. In FIG. 2, the condensate cooling heat exchanger 8 in FIG. 1 is omitted, and the makeup water supply pipe 14 is installed on the downstream side of the process heat exchanger 5 in the pipe 12.

<Second Embodiment>
FIG. 3 is a system diagram for explaining a condensate treatment method and a condensate treatment apparatus according to the second embodiment.
(Condensate treatment equipment and boiler equipment)
First, the boiler equipment provided with the condensate treatment apparatus which concerns on this Embodiment is demonstrated. The outlet of the boiler 1 is connected to the inlet of the power generation turbine 2 through the pipe 31, and the outlet of the power generation turbine 2 is connected to the inlet of the anion exchange tower 3 through the pipe 32. The outlet is connected to the inlet of the boiler 1 via a pipe 33. In the middle of the pipe 32, the process heat exchanger 5 and the makeup water supply pipe 34 are connected. In the middle of the pipe 34, a cation exchange resin tower 6 and a decarboxylation tower 7 are provided in this order from the side far from the pipe 32. The drug tank 4 is connected to the middle of the pipe 33 via the pipe 35. A blow pipe 36 is connected to the boiler 1.

A cation exchange resin is accommodated in the cation resin exchange tower 6. The cation exchange resin is not particularly limited, and known ones can be used, but amine-type cation exchange resins such as H-type, NH ₄ type, monoethanolamine (ETA) and the like are preferably used.
The boiler equipment 40 is comprised by these apparatuses 1-4, 6-7 and the piping 31-36. The anion exchange resin 3, the chemical tank 4, and the pipes 32, 33, 35 constitute a condensate treatment device 41. These cation exchange resin tower 6, decarboxylation tower 7 and anion exchange resin tower 3 constitute a two-bed / three-column pure water production apparatus. The devices 1 to 4 are the same as those in the first embodiment.

(Condensate treatment method and operation method of boiler equipment)
Next, the condensate treatment method according to the present embodiment will be described. Condensate flowing out from the anion exchange tower 3 is supplied to the boiler 1 as boiler feed water after the chemical in the chemical tank 4 is added for pH adjustment. Details such as the pH of the boiler feed water, the type of chemicals, and the amount added are the same as those in the first embodiment.
Next, in the same manner as in the first embodiment, steam produced in the boiler 1 is supplied to the power generation turbine 2 and used for power generation, and a part of boiler can water is blown. The details of the concentration, blow rate, and condensate recovery rate are the same as in the first embodiment.

The steam flowing out of the power generation turbine 2 becomes condensate through the process heat exchanger 5 and is mixed with make-up water and then supplied to the anion exchange tower 3.
Here, the makeup water passes through the cation exchange resin tower 6 to remove cations (Na ⁺ , Mg ²⁺ , Ca ^2+, etc.), and further passes through the decarboxylation tower 7 to form carbonate ions (HCO ³⁻ ) Is removed, it flows into the pipe 32 and is mixed with the condensate. In this way, since the makeup water is mixed with the boiler water after the cations and carbonate ions are removed, cations are prevented from being brought in from the makeup water. In addition, since condensate is not passed through the cation exchange resin tower 6 and the decarbonation tower 7, the load on the towers 6 and 7 is small, and the service life is extended.

The mixed water of the condensate and make-up water is supplied into the anion exchange resin tower 3, and the organic acid in the mixed water is removed in the same manner as in the first embodiment.
The mixed water subjected to the anion exchange treatment is supplied to the boiler 1 again after the chemical is added as described above. In this way, boiler supply and condensate circulates in the boiler facility 40.

  In the present embodiment, since the condensate flowing out from the process heat exchanger 5 is cooled by make-up water and then supplied into the anion exchange resin tower 3, the condensate temperature is high (for example, exceeds 60 ° C.). Even in this case, it is possible to prevent thermal deterioration of the anion exchange resin without providing a heat exchanger for cooling the condensate.

<Modification of Second Embodiment>
In FIG. 3, there are no particular limitations on the place where the chemical is added, and it may be added in the middle of the pipe 31, upstream or downstream of the pipe 32 where the pipe 34 is connected. It may also be added at these two or more locations.
The point which may add chemical | medical agents other than an amine etc. is the same as that of 1st Embodiment.
The above embodiment is an example of the present invention, and the present invention is not limited to the above embodiment. For example, a bypass line of the anion exchange resin tower 3 may be provided so that a part of the condensate is not supplied to the anion exchange resin tower 3. Thereby, the load of the anion exchange resin tower 3 is reduced. The decarboxylation tower 7 may be omitted.

EXAMPLES Hereinafter, although an Example demonstrates this invention further in detail, this invention is not limited to a following example, unless the summary is exceeded.
Comparative Example 1
<First operation (without addition of acetic acid)>
Operation was performed using the test boiler equipment for testing shown in FIG. 4 is obtained by replacing the anion exchange resin tower 3 with a heating deaerator 50 (exit degassing capacity 0.007 mg / L) in FIG.
Pure water (ion exchange water) was used as boiler water and make-up water, and a boiler having a boiler pressure of 11 MPa and a boiler temperature of 320 ° C. was used. The temperature of the makeup water was 20 ° C. The concentration was 100 times, the condensate recovery rate was 70%, and the blow rate was 1%.
As the drug, sodium phosphate (Na / PO ₄ molar ratio: 2.7) and 3-methoxypropylamine (MOPA) were used. Sodium phosphate was added to the boiler feed water so as to be 0.02 mg / L in terms of phosphate ions. MOPA was added at 0.4 mg / L to the boiler feed water so that the pH of the boiler feed water and condensate was 9.1.
As a result, the pH of the boiler can water was 9.3.

<Second operation (with acetic acid added)>
Subsequently, 0.2 mg / L of acetic acid was added to the make-up water, assuming an organic acid generated by thermal decomposition of a trace amount of organic matter derived from the make-up water in the boiler water.
As a result, the pH of the boiler feed water and condensate decreased to 8.9, and the pH of the boiler can water (water in the boiler 1) decreased to 8.7.

Comparative Example 2
In the second operation of Comparative Example 1, when the amount of MOPA added was increased so that the pH of the boiler feed water was 9.1, the amount of MOPA added required 0.52 mg / L. At this time, the pH of the boiler water was 8.8.

Comparative Example 3
As the test boiler equipment for testing, the one shown in FIG. 5 was used. The test boiler equipment for testing of FIG. 5 is a mixed bed in which an anion exchange resin and a cation exchange resin are accommodated between the connection portion of the heat exchanger 5 and the makeup water 14 in the pipe 12 in FIG. The one equipped with a desalting tower (polisher) 51 of the formula was used.
In the second operation of Comparative Example 1, when the total amount of condensate was passed through the polisher while controlling the amine addition amount so as to maintain the pH 9.1 of the boiler feed water, the amine addition amount was 1.44 mg / Large increase to L. At this time, the pH of the boiler can water was 9.2.
The temperature of the boiler condensate was 80 ° C., which exceeded 60 ° C., which is the heat resistant temperature of the resin. Therefore, it was necessary to pass cooling water through the heat exchanger and to reduce the condensate temperature to 60 ° C. or lower.

Example 1
As the test boiler equipment for testing, the one shown in FIG. 6 was used. The test boiler equipment for testing of FIG. 6 is the same as that of FIG. 4 except that the heat exchanger 5 is omitted and the anion exchange resin tower is provided between the connection portion of the make-up water 14 in the pipe 12 and the heating deaerator 50. What provided 52 was used. As the anion exchange resin tower 52, a column filled with 50 L of OH type anion exchange resin (manufactured by Mitsubishi Chemical Corporation, “DIAION PA312LOH”) was used.
Pure water (ion exchange water) was used as boiler water and make-up water, and a boiler having a boiler pressure of 11 MPa and a boiler temperature of 320 ° C. was used. The temperature of the makeup water was 20 ° C. The concentration was 100 times, the condensate recovery rate was 70%, and the blow rate was 1%.
As the drug, sodium phosphate (Na / PO ₄ molar ratio 2.7) and MOPA were used. Sodium phosphate was added to the boiler feed water so as to be 0.02 mg / L in terms of phosphate ions. MOPA was added at 0.4 mg / L to the boiler feed water so that the pH of the boiler feed water was 9.1.
Furthermore, 0.2 mg / L acetic acid was added to the make-up water, assuming an organic acid generated by thermal decomposition of a trace amount of organic matter derived from the make-up water in the boiler water.

As a result, the addition amount of MOPA necessary for adjusting the pH of boiler feed water to 9.1 was 0.4 mg / L. At this time, the pH of the boiler can water rose to 9.2, and the anticorrosion tendency increased.
In addition, the temperature of the condensate supplied to the anion exchange tower was 60 ° C. That is, the temperature of the condensate from the power generation turbine 2 was 80 ° C. Further, as described above, the condensate recovery rate is 70%, and makeup water having a temperature of 20 ° C. is mixed with the condensate from the power generation turbine 2 by the amount of boiler water (30%) discharged outside the system. The temperature of the condensate was 60 ° C. Since this temperature is lower than the heat resistant temperature (80 ° C.) of the anion exchange resin, it was not necessary to install a heat exchanger and cool the condensate.

  From the above, it was confirmed that by installing an anion exchange resin tower, it is possible not only to prevent a decrease in the pH of boiler water, but also to increase the corrosion resistance tendency. From this, it is inferred that the organic acid is well removed by the anion exchange resin tower. Moreover, it was confirmed that the amount of amine added can be greatly reduced by installing an anion exchange resin tower as compared with the case of installing a polisher (mixed bed type resin layer).

DESCRIPTION OF SYMBOLS 1 Boiler 2 Power generation turbine 3 Anion exchange resin tower 4 Chemical tank 5 Process heat exchanger 6 Cation exchange resin tower 7 Decarbonation tower 8 Heat exchanger for condensate cooling 50 Heating deaerator 51 Mixed bed type desalting tower (Polisher )
52 Anion Exchange Resin Tower

Claims (8)

  A condensate treatment method in which at least a part of a condensate of a boiler is treated with an ion exchange resin and then supplied to the boiler, wherein the ion exchange resin is made of an anion exchange resin.   The condensate treatment method according to claim 1, wherein at least a part of the condensate is treated with the anion exchange resin after being mixed with makeup water.   The condensate treatment method according to claim 2, wherein the makeup water is treated with a cation exchange resin and then mixed with at least a part of the condensate.   The condensate treatment method according to claim 2, wherein the makeup water is treated with a cation exchange resin, decarboxylated, and then mixed with at least a part of the condensate.   Condensate having an ion exchange tower containing ion exchange resin, a condensate pipe for supplying boiler condensate to the ion exchange tower, and a water supply pipe for supplying treated water treated by the ion exchange tower to the boiler A condensate treatment apparatus, wherein the ion exchange resin is an anion exchange resin.   The condensate treatment apparatus according to claim 5, further comprising a makeup water supply pipe connected to the condensate pipe.   The condensate treatment apparatus according to claim 6, wherein a cation exchange tower containing a cation exchange resin is provided in the middle of the makeup water supply pipe.   7. The recovery according to claim 6, wherein a cation exchange tower and a decarboxylation tower in which a cation exchange resin is accommodated are provided in this order from a side far from a connection location with the water supply pipe in the middle of the makeup water supply pipe. Water treatment equipment.

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