WO2018207492A1 - Boiler water treatment apparatus and treatment method - Google Patents

Boiler water treatment apparatus and treatment method Download PDF

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Publication number
WO2018207492A1
WO2018207492A1 PCT/JP2018/013228 JP2018013228W WO2018207492A1 WO 2018207492 A1 WO2018207492 A1 WO 2018207492A1 JP 2018013228 W JP2018013228 W JP 2018013228W WO 2018207492 A1 WO2018207492 A1 WO 2018207492A1
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Prior art keywords
boiler
water
pure water
toc
supply line
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PCT/JP2018/013228
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French (fr)
Japanese (ja)
Inventor
隆史 仲本
和巳 塚本
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栗田工業株式会社
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Publication of WO2018207492A1 publication Critical patent/WO2018207492A1/en

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/30—Treatment of water, waste water, or sewage by irradiation
    • C02F1/32—Treatment of water, waste water, or sewage by irradiation with ultraviolet light
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/42—Treatment of water, waste water, or sewage by ion-exchange
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22B—METHODS OF STEAM GENERATION; STEAM BOILERS
    • F22B37/00—Component parts or details of steam boilers
    • F22B37/02—Component parts or details of steam boilers applicable to more than one kind or type of steam boiler
    • F22B37/48—Devices for removing water, salt, or sludge from boilers; Arrangements of cleaning apparatus in boilers; Combinations thereof with boilers
    • F22B37/52—Washing-out devices
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F22—STEAM GENERATION
    • F22D—PREHEATING, OR ACCUMULATING PREHEATED, FEED-WATER FOR STEAM GENERATION; FEED-WATER SUPPLY FOR STEAM GENERATION; CONTROLLING WATER LEVEL FOR STEAM GENERATION; AUXILIARY DEVICES FOR PROMOTING WATER CIRCULATION WITHIN STEAM BOILERS
    • F22D11/00—Feed-water supply not provided for in other main groups
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02A—TECHNOLOGIES FOR ADAPTATION TO CLIMATE CHANGE
    • Y02A20/00—Water conservation; Efficient water supply; Efficient water use
    • Y02A20/124—Water desalination
    • Y02A20/131—Reverse-osmosis

Definitions

  • the present invention relates to an apparatus and method for treating boiler water of power generation equipment such as commercial thermal power, IPP power generation equipment or industrial thermal power generation equipment.
  • IPP power generation independent power generation business
  • pure water is produced from industrial water or the like by pretreatment (such as agglomeration solid-liquid separation and desalination treatment), and steam is generated from the pure water using a high pressure boiler to generate power.
  • pretreatment such as agglomeration solid-liquid separation and desalination treatment
  • steam is generated from the pure water using a high pressure boiler to generate power.
  • boiler blow water is collected, desalted, and reused as pure water for power generation (Patent Documents 1 to 3).
  • the boiler water quality is managed in the power generation facility.
  • the electrical conductivity of boiler water after being treated with an ion exchange resin is managed.
  • raw water contains TOC more than expected (for example, TOC 200 ppb or more), or when organic substances are excessively eluted from ion-exchange resin in pre-treatment pure water production, the electrical conductivity of boiler water exceeds the control value. Resulting in.
  • An object of the present invention is to provide a boiler water treatment apparatus and a treatment method capable of stably supplying high-quality pure water to a boiler even when the TOC of raw water or pretreatment water is high in concentration.
  • the boiler water treatment device of the present invention is a boiler water treatment device having a pretreatment device for producing pure water by treating raw water, and a pure water supply line for supplying pure water from the pretreatment device to the boiler.
  • the take-out unit is provided in a pure water tank of a pure water supply line.
  • the TOC removing unit includes an RO device or a UV oxidation device and an ion exchange device.
  • the boiler water treatment apparatus includes a measuring unit for measuring the TOC concentration of pure water in the pure water take-out unit or the upstream side of the pure water supply line, and a measured value of the measuring unit is a predetermined value.
  • the TOC removal unit starts the TOC removal, or the pure water supply amount control unit increases the pure water supply amount to the TOC removal unit.
  • a boiler water treatment apparatus includes condensate demineralization means for desalinating boiler blow water discharged from the boiler after exhaust steam from the boiler is condensed, and boiler blow water from the boiler A boiler blow water introduction line to be introduced into the condensate demineralization means, and a condensate for returning the condensate demineralized water desalted by the condensate demineralization means to the take-out section or a pure water supply line upstream of the extraction section. And a desalted water return line.
  • the boiler water treatment apparatus includes an RO device as the TOC removing unit, and a heat exchanger for exchanging heat between the RO concentrated water and the boiler blow water of the RO device is provided in the boiler blow water introduction line. Prepare.
  • the boiler water treatment method of the present invention is a boiler water treatment method in which raw water is treated with a pretreatment device to produce pure water, and pure water from the pretreatment device is supplied to the boiler via a pure water supply line. , Removing a part of the pure water from the pure water supply line from the take-out part, and removing the TOC by the TOC removing means, and returning the treated water to the take-out part or the pure water supply line on the upstream side thereof. It is a feature.
  • the TOC removing unit includes an RO device or a UV oxidation device and an ion exchange device.
  • the TOC concentration of pure water in the pure water supply line on the upstream side with respect to the take-out part is measured, and the TOC removal is performed when the measured value is a predetermined value or more.
  • the TOC removal by the means is started, or the amount of pure water supplied to the TOC removal means is increased.
  • the boiler blow water discharged from the boiler after the exhaust steam from the boiler is condensed is desalted by the condensate demineralization means, and dehydrated by the condensate demineralization means.
  • the salt-treated condensate demineralized water is returned to the extraction section or the pure water supply line upstream of the extraction section.
  • the TOC removing unit includes an RO device, and heat exchange is performed between the RO concentrated water of the RO device and the boiler blow water supplied to the condensate demineralization unit. Then, the boiler blow water is cooled.
  • the TOC removal means is not provided in the pure water supply line (main line) for supplying pure water from the pretreatment device to the boiler, but the TOC removal line (offline) branched from the pure water supply line. Removal means are provided. Therefore, the TOC removing unit can be controlled separately from the pure water supply control in the pure water supply line (main line).
  • the TOC removal operation when the TOC load of raw water is low, the TOC removal operation can be temporarily suspended. Further, even when the pure water supply line is in a pure water supply operation, the maintenance of the TOC removing means can be performed.
  • the RO concentrated water in the TOC removal line is used as cooling water for boiler blow water.
  • FIG. 1 is a flowchart of a boiler water treatment apparatus according to an embodiment of the present invention.
  • FIG. 2 is a flowchart of a boiler water treatment apparatus according to another embodiment.
  • FIG. 3 is a flowchart of the boiler water treatment apparatus according to the comparative example.
  • FIG. 1 is a flowchart of the boiler water treatment apparatus according to the first embodiment.
  • Industrial water industrial water
  • pure water tank 3 corresponding to a takeout portion
  • Pure water in the pure water tank 3 is supplied to a boiler of a power generator 6 such as an IPP power generator via a pipe 5 having a pump 4.
  • the pure water supply line has a pipe 2, a pure water tank 3, a pump 4 and a pipe 5.
  • Boiler blow water generated in the boiler of the power generation device 6 is introduced into the condensate demineralizer 10 through the introduction line having the pipe 7, the first heat exchanger 8B, the cooling means 8A, and the pipe 9, and is desalted.
  • the condensate desalination apparatus 10 includes reverse osmosis membrane separation apparatuses (RO apparatuses) 11 and 12 arranged in a plurality of stages (two stages in this embodiment), and an electric desalination apparatus 13. Have.
  • the boiler blow water is desalted by RO treatment and electric desalination treatment to become pure water, and is returned to the pure water tank 3 via the pipe 14.
  • a TOC removal line is provided in order to take out a part of pure water in the pure water tank 3 and perform TOC removal treatment and desalination treatment.
  • Pure water in the pure water tank 3 is supplied to the RO device 18 via the pipe 15, the second heat exchanger 16, and the pump 17, and RO permeated water is returned to the pure water tank 3 via the pipe 19.
  • the RO concentrated water is supplied to the first heat exchanger 8B via the pipe 20, and after heat exchange with the boiler blow water, the pre-treatment device 1 or upstream of the raw water pipe or the raw water tank is supplied via the pipe 21. Returned or discharged out of the system.
  • the second heat exchanger 16 heats pure water supplied from the pure water tank 3 to the RO device 18.
  • the first heat exchanger 8B cools and lowers the temperature of the boiler blow water sent to the condensate demineralizer 10.
  • the concentrated water from the RO device 18 is passed through the first heat exchanger 8B to the low temperature fluid side.
  • the pump 17 is operated when necessary, and the pure water in the pure water tank 3 is subjected to RO treatment by the RO device 18, whereby the quality of pure water in the pure water tank 3 is predetermined. Can be kept in range.
  • the RO treatment efficiency can be increased by heating the pure water supplied to the RO device 18 with the second heat exchanger 16.
  • the water temperature in the pure water tank 3 increases.
  • the pipe 15 is connected to the pure water tank 3 as a take-out portion, but the pipe 15 may be connected to the pipe 5 on the downstream side of the pure water tank 3. In this case, the branch point becomes the takeout part.
  • FIG. 2 is a flowchart of the boiler water treatment apparatus according to the second embodiment.
  • a TOC removing device for maintaining the quality of pure water in the pure water tank 3 a UV (ultraviolet) oxidation device 25 and an ion exchange device 26 are installed instead of the RO device 18 in FIG.
  • the ion exchange resin is preferably an anion exchange resin or a mixed bed resin.
  • UV oxidation apparatus e.g., a low-pressure UV oxidation apparatus
  • the organic material by irradiating the (pure water from the pure water tank 3) the UV treated water and organic acids to CO 2.
  • the organic acid, CO 2 and the like generated by the decomposition are removed by the ion exchange device 26 at the subsequent stage. Pure water having a low organic matter concentration that has passed through the ion exchange device 26 is returned from the pipe 19 to the pure water tank 3.
  • the pipes 20 and 21 for supplying the RO concentrated water to the first heat exchanger 8B are not installed. Cooling water introduced from outside the system is passed through the first heat exchanger 8B on the low temperature fluid side.
  • Boiler blow water from the boiler of the power generation device 6 is sent to the condensate demineralizer 10 through an introduction line having the pipe 7, the first heat exchanger 8B, the cooling means 8A, and the pipe 9.
  • Other configurations are the same as those in FIG. 1, and the same reference numerals indicate the same parts.
  • Pretreatment device 1 removes the raw water such as industrial water (city water, groundwater, etc.) after performing coagulation treatment, solid-liquid separation (precipitation separation, pressurized flotation separation, etc.) and two-layer filtration sequentially. Pure water is produced by performing a salt treatment (treatment with a cation exchange resin tower, a decarboxylation tower, an anion exchange resin tower, a mixed bed resin tower, an electric desalination apparatus, or the like).
  • a salt treatment treatment with a cation exchange resin tower, a decarboxylation tower, an anion exchange resin tower, a mixed bed resin tower, an electric desalination apparatus, or the like.
  • Pure water tank 3 In the pure water tank 3, pure water produced by the pretreatment is stored, and the water quality and the amount of water are adjusted.
  • TOC removal means When the TOC concentration contained in raw water such as industrial water is high, it may be difficult to reduce the TOC concentration to a predetermined value or less (for example, less than 100 ppb) by pretreatment. When the TOC concentration is 100 ppb or more, there is a concern that a burden on the boiler becomes large and a failure may occur in the future.
  • the water temperature varies depending on the season and climate (for example, 5 to 35 ° C). When the water temperature is 15 ° C. or less, the load on the power generation boiler increases and the amount of fuel used increases.
  • the pure water collected from the pure water tank 3 constituting the pure water supply line is supplied to the RO device 18 so that the TOC of pure water in the pure water tank 3 is always maintained at a predetermined value or less (for example, 100 ppb or less).
  • the TOC removal process is performed by the TOC removal means comprising the UV oxidation device 25 and the ion exchange device 26.
  • the TOC removing means By using a physicochemical means as the TOC removing means, it is possible to prevent impurities from remaining in the treated water.
  • the TOC removal means By installing the TOC removal means in the TOC removal line branched from the pure water supply line, for example, control and maintenance different from the pure water supply line are possible, such as being unaffected by the stoppage of water flow due to the membrane backwashing.
  • the TOC removing means can be easily installed in an existing boiler water supply device by additional work.
  • the TOC concentration measuring means and the pump 17 are interlocked, and when the measured value of the TOC concentration measuring means exceeds a predetermined value, the pump 17 is operated to supply water to the TOC removing means, and the TOC.
  • a removal process may be performed.
  • An on-off valve is provided in the pipe 15, and this on-off valve is interlocked with the TOC concentration measuring means to open the on-off valve when the measured value of the TOC concentration measuring means is a predetermined value or more and supply pure water to the TOC removing means. You may make it perform a TOC removal process.
  • the pump 17 is stopped or the on-off valve is closed to stop the supply of pure water to the TOC removing means.
  • the amount of pure water supplied to the TOC removing means may be controlled. For example, by interlocking the TOC concentration measuring means and the pump 17, when the measured value of the TOC concentration measuring means exceeds a predetermined value, the rotational speed of the pump 17 is increased to increase the amount of pure water supplied to the TOC removing means. The amount of pure water to be subjected to the TOC removal process may be increased.
  • a flow rate adjusting valve is provided in the pipe 15, and this flow rate adjusting valve is linked to the TOC concentration measuring means.
  • the opening of the flow adjusting valve is increased to remove the TOC.
  • the amount of pure water supplied to the means may be increased to increase the amount of pure water subjected to the TOC removal process.
  • the pure water supply amount to the TOC removing means is reduced by reducing the rotational speed of the pump 17 or reducing the opening of the flow rate adjusting valve.
  • the required amount of pure water can be processed by the TOC removing means by controlling the presence or the amount of pure water supplied to the TOC removing means. Costs related to the TOC removal process can be reduced.
  • the control of whether or not the pure water is supplied to the TOC removing means or the increase / decrease in the supply amount is performed by inputting the measured value of the TOC concentration of the TOC concentration measuring means and outputting a control signal to the pump or valve based on the measured value. It can be performed automatically by the control device.
  • the power generation device 6 there are various types such as an IPP power generation device equipped with a high-pressure boiler.
  • Boiler blow water discharge line to condensate demineralization means to condensate return line The boiler steam condensate is generally at a high temperature (for example, 70 to 97 ° C), and after being discharged from the boiler as boiler blow water, cooling means 8A (sealed) After cooling to about 20 to 40 ° C. by a cooling tower, a heat exchanger, etc., it is supplied to the condensate demineralizer 10.
  • First heat exchanger 8B As shown in FIG. 1, when the RO device 18 is used as the TOC removing means, the RO concentrated water at a room temperature (5 to 35 ° C.) is discharged, so this RO concentrated water is provided in the first stage of the cooling means 8A. 1 Water is passed through the heat exchanger 8B to exchange heat with the boiler blow water, and the boiler blow water is precooled to about 50 to 70 ° C. Thereby, the load of the cooling means 8A provided in the front stage of the condensate demineralizer 10 is reduced.
  • Second heat exchanger 16 When the water temperature of the pure water tank 3 is likely to drop to a predetermined value or lower (for example, 15 ° C. or lower), the water supplied from the TOC removing unit is heated by exchanging heat with hot water in the second heat exchanger 16. Thereby, it is possible to remove the TOC efficiently by the TOC removing means. If the water temperature of the pure water tank 3 is maintained at 20 to 35 ° C., for example, the burden on the high-pressure boiler of the IPP power generation facility can be reduced.
  • a predetermined value or lower for example, 15 ° C. or lower
  • the valve may be switched so as to supply hot water to the second heat exchanger 16 and the temperature may be controlled by this mechanism.
  • the flow rate may be controlled so as to adjust the supply flow rate to the second heat exchanger 16 based on the measured water temperature.
  • Example 1 Chiba Prefecture industrial water (TOC concentration 2 to 3 ppm; water temperature 10 ° C.) was treated by the boiler water treatment device shown in FIG. 1 and supplied to the boiler of the IPP power generation device 6, and boiler blow water was collected.
  • the pretreatment apparatus 1 pure water was produced by performing agglomeration treatment, pressurized flotation separation, two-layer filtration, two-bed three-column ion exchange (cation exchange, decarboxylation, anion exchange). The main conditions are shown below and in Table 1. The results are shown in Table 1.
  • Average supply amount of industrial water (average flow rate in pipe 2): 35 m 3 / hr Pure water tank 3 volume: 400m 3 Average amount of water supply to the IPP power generation boiler (average flow rate in the pipe 5): 35 m 3 / hr Boiler blow water average flow rate (average flow rate in pipe 7): 10 to 12 m 3 / hr RO device 18 average water supply amount (average flow rate in pipe 15): 34 m 3 / hr RO device 18 average permeate flow rate (average flow rate in pipe 19): 30 m 3 / hr 1st heat exchanger 8B feed water average flow rate: 10-12m 3 / hr Cooling means 8A water supply average flow rate: 10-12 m 3 / hr Second heat exchanger 16 average feed water flow rate: 34 m 3 / hr
  • Example 2 The operation was performed under the same conditions as in Example 1 except that the boiler water treatment apparatus shown in FIG. The results are shown in Table 1.
  • Example 3 In Example 1, the 2nd heat exchanger 16 was abbreviate
  • FIG. The results are shown in Table 1.
  • Example 4 In Example 1, the operation was performed under the same conditions as in Example 1 except that the pipes 20 and 21 and the first heat exchanger 8B were omitted and the boiler blow water was not preliminarily cooled with the RO concentrated water. The results are shown in Table 1.
  • Example 1 In Example 1, the piping 15 for removing the TOC, the second heat exchanger 16, the pump 17, the RO device 18, the piping 19, the piping 20, 21 and the first heat exchanger 8B are omitted, and the flow of FIG. The operation was performed under the same conditions as in Example 1 except that. The results are shown in Table 1.
  • the TOC concentration of boiler feed water is lower than that in Comparative Example 1, and the load on the boiler is reduced.
  • the TOC removal rate in the same RO apparatus is higher in Examples 1 and 4 in which the TOC removal line was not preheated than in Example 3 in which the TOC removal line was not preliminarily performed.
  • the load on the subsequent boiler is reduced.
  • the load on the subsequent cooling means is reduced in the first to third embodiments in which the boiler blow water was not preliminarily cooled in the first to third embodiments.

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Abstract

Industrial water is supplied via a pretreatment device 1 and a pure water tank 3 to a boiler of an electric power generating apparatus 6. Boiler blowdown water is demineralized by a condensate demineralizing apparatus 10 and returned to the pure water tank 3. A portion of the pure water in the pure water tank 3 is supplied to an RO device 18 and the RO permeate is returned to the pure water tank 3. The RO concentrate is conveyed via piping 20 to a first heat exchanger 8B.

Description

ボイラ水処理装置および処理方法Boiler water treatment apparatus and treatment method
　本発明は、事業用火力、ＩＰＰ発電設備或いは産業用火力発電設備等の発電設備のボイラ水を処理する装置及び方法に関する。 The present invention relates to an apparatus and method for treating boiler water of power generation equipment such as commercial thermal power, IPP power generation equipment or industrial thermal power generation equipment.
　コンビナートにおいてＩＰＰ発電（独立系発電事業）の実施が広がっている。ＩＰＰ等の発電設備では、工業用水等から前処理（凝集固液分離と脱塩処理など）により純水を製造し、この純水を用いて高圧ボイラにより蒸気を発生させて発電が行われる。発電設備では、ボイラブロー水を回収し、脱塩処理した後に発電用の純水として再利用する（特許文献１～３）。 Implementation of IPP power generation (independent power generation business) is spreading in the complex. In power generation equipment such as IPP, pure water is produced from industrial water or the like by pretreatment (such as agglomeration solid-liquid separation and desalination treatment), and steam is generated from the pure water using a high pressure boiler to generate power. In the power generation facility, boiler blow water is collected, desalted, and reused as pure water for power generation (Patent Documents 1 to 3).
　発電施設内では、ボイラ水の水質を管理している。特に、腐食防止の為、イオン交換樹脂にて処理した後のボイラ水の電気伝導度を管理している。原水にＴＯＣが想定以上に含まれていた場合（例えばＴＯＣ２００ｐｐｂ以上）、または前処理の純水製造におけるイオン交換樹脂から有機物が過度に溶出した場合は、ボイラ水の電気伝導度が管理値を超過してしまう。 The boiler water quality is managed in the power generation facility. In particular, in order to prevent corrosion, the electrical conductivity of boiler water after being treated with an ion exchange resin is managed. When raw water contains TOC more than expected (for example, TOC 200 ppb or more), or when organic substances are excessively eluted from ion-exchange resin in pre-treatment pure water production, the electrical conductivity of boiler water exceeds the control value. Resulting in.
特開２００７－２６８３９７号公報Japanese Patent Laid-Open No. 2007-26897 特開２０１０－２１６７６２号公報JP 2010-216762 A 特開２０１５－１１７９１３号公報Japanese Patent Laying-Open No. 2015-117913
　本発明は、原水又は前処理水のＴＯＣが高濃度の場合でも安定して高品質の純水をボイラに給水することができるボイラ水処理装置及び処理方法を提供することを目的とする。 An object of the present invention is to provide a boiler water treatment apparatus and a treatment method capable of stably supplying high-quality pure water to a boiler even when the TOC of raw water or pretreatment water is high in concentration.
　本発明のボイラ水処理装置は、原水を処理して純水を製造する前処理装置と、該前処理装置からの純水をボイラへ供給する純水供給ラインとを有するボイラ水処理装置において、該純水供給ラインから純水の一部を取り出し部から取り出してＴＯＣ除去手段でＴＯＣ除去処理し、この処理水を該取り出し部又はそれよりも上流側の該純水供給ラインに戻すＴＯＣ除去ラインを備えたことを特徴とするものである。 The boiler water treatment device of the present invention is a boiler water treatment device having a pretreatment device for producing pure water by treating raw water, and a pure water supply line for supplying pure water from the pretreatment device to the boiler. A TOC removal line in which a part of pure water is taken out from the take-out portion from the pure water supply line, subjected to TOC removal by the TOC removing means, and this treated water is returned to the take-out portion or the pure water supply line on the upstream side thereof. It is characterized by comprising.
　本発明の一態様では、該取り出し部は、純水供給ラインの純水タンクに設けられる。 In one aspect of the present invention, the take-out unit is provided in a pure water tank of a pure water supply line.
　本発明の一態様では、前記ＴＯＣ除去手段は、ＲＯ装置を有するか、又はＵＶ酸化装置及びイオン交換装置を有する。 In one aspect of the present invention, the TOC removing unit includes an RO device or a UV oxidation device and an ion exchange device.
　本発明の一態様のボイラ水処理装置は、前記純水の取り出し部又はそれよりも上流側の前記純水供給ラインの純水のＴＯＣ濃度の測定手段と、該測定手段の測定値が所定値以上のときに前記ＴＯＣ除去手段によるＴＯＣ除去を開始するか、又はＴＯＣ除去手段への純水供給量を増加させる純水供給量制御手段を備える。 The boiler water treatment apparatus according to one aspect of the present invention includes a measuring unit for measuring the TOC concentration of pure water in the pure water take-out unit or the upstream side of the pure water supply line, and a measured value of the measuring unit is a predetermined value. At the time described above, the TOC removal unit starts the TOC removal, or the pure water supply amount control unit increases the pure water supply amount to the TOC removal unit.
　本発明の一態様のボイラ水処理装置は、前記ボイラからの排気蒸気が凝縮されて該ボイラから排出されたボイラブロー水を脱塩処理する復水脱塩手段と、該ボイラからのボイラブロー水を該復水脱塩手段に導入するボイラブロー水導入ラインと、該復水脱塩手段で脱塩処理された復水脱塩水を前記取り出し部又はそれよりも上流側の純水供給ラインに返送する復水脱塩水返送ラインとを備える。 A boiler water treatment apparatus according to an aspect of the present invention includes condensate demineralization means for desalinating boiler blow water discharged from the boiler after exhaust steam from the boiler is condensed, and boiler blow water from the boiler A boiler blow water introduction line to be introduced into the condensate demineralization means, and a condensate for returning the condensate demineralized water desalted by the condensate demineralization means to the take-out section or a pure water supply line upstream of the extraction section. And a desalted water return line.
　本発明の一態様のボイラ水処理装置は、前記ＴＯＣ除去手段としてＲＯ装置を有しており、該ＲＯ装置のＲＯ濃縮水とボイラブロー水とを熱交換させる熱交換器を前記ボイラブロー水導入ラインに備える。 The boiler water treatment apparatus according to an aspect of the present invention includes an RO device as the TOC removing unit, and a heat exchanger for exchanging heat between the RO concentrated water and the boiler blow water of the RO device is provided in the boiler blow water introduction line. Prepare.
　本発明のボイラ水処理方法は、原水を前処理装置で処理して純水を製造し、該前処理装置からの純水を純水供給ラインを経由してボイラへ供給するボイラ水処理方法において、該純水供給ラインから純水の一部を取り出し部から取り出してＴＯＣ除去手段でＴＯＣ除去処理し、この処理水を該取り出し部又はそれよりも上流側の該純水供給ラインに戻すことを特徴とするものである。 The boiler water treatment method of the present invention is a boiler water treatment method in which raw water is treated with a pretreatment device to produce pure water, and pure water from the pretreatment device is supplied to the boiler via a pure water supply line. , Removing a part of the pure water from the pure water supply line from the take-out part, and removing the TOC by the TOC removing means, and returning the treated water to the take-out part or the pure water supply line on the upstream side thereof. It is a feature.
　本発明の一態様のボイラ水処理方法では、前記ＴＯＣ除去手段は、ＲＯ装置を有するか、又はＵＶ酸化装置及びイオン交換装置を有する。 In the boiler water treatment method according to one aspect of the present invention, the TOC removing unit includes an RO device or a UV oxidation device and an ion exchange device.
　本発明の一態様のボイラ水処理方法では、前記取り出し部又はそれよりも上流側の前記純水供給ラインの純水のＴＯＣ濃度を測定し、該測定値が所定値以上のときに前記ＴＯＣ除去手段によるＴＯＣ除去を開始するか、又はＴＯＣ除去手段への純水供給量を増加させる。 In the boiler water treatment method according to an aspect of the present invention, the TOC concentration of pure water in the pure water supply line on the upstream side with respect to the take-out part is measured, and the TOC removal is performed when the measured value is a predetermined value or more. The TOC removal by the means is started, or the amount of pure water supplied to the TOC removal means is increased.
　本発明の一態様のボイラ水処理方法では、前記ボイラからの排気蒸気が凝縮されて該ボイラから排出されたボイラブロー水を復水脱塩手段で脱塩処理し、該復水脱塩手段で脱塩処理された復水脱塩水を前記取り出し部又はそれよりも上流側の純水供給ラインに返送する。 In the boiler water treatment method of one aspect of the present invention, the boiler blow water discharged from the boiler after the exhaust steam from the boiler is condensed is desalted by the condensate demineralization means, and dehydrated by the condensate demineralization means. The salt-treated condensate demineralized water is returned to the extraction section or the pure water supply line upstream of the extraction section.
　本発明の一態様のボイラ水処理方法では、前記ＴＯＣ除去手段はＲＯ装置を有しており、該ＲＯ装置のＲＯ濃縮水と前記復水脱塩手段に供給されるボイラブロー水とを熱交換して、該ボイラブロー水を冷却する。 In the boiler water treatment method of one aspect of the present invention, the TOC removing unit includes an RO device, and heat exchange is performed between the RO concentrated water of the RO device and the boiler blow water supplied to the condensate demineralization unit. Then, the boiler blow water is cooled.
　本発明では、前処理装置からの純水をボイラに供給する純水供給ライン（メインライン）にＴＯＣ除去手段を設けるのではなく、該純水供給ラインから分岐したＴＯＣ除去ライン（オフライン）にＴＯＣ除去手段を設けている。そのため、ＴＯＣ除去手段を、純水供給ライン（メインライン）での純水供給制御とは別に制御することができる。 In the present invention, the TOC removal means is not provided in the pure water supply line (main line) for supplying pure water from the pretreatment device to the boiler, but the TOC removal line (offline) branched from the pure water supply line. Removal means are provided. Therefore, the TOC removing unit can be controlled separately from the pure water supply control in the pure water supply line (main line).
　例えば、本発明では、原水のＴＯＣ負荷が低いときには、ＴＯＣ除去運転を一時中断することができる。また、純水供給ラインが純水供給作動しているときでも、ＴＯＣ除去手段のメンテナンスが可能である。 For example, in the present invention, when the TOC load of raw water is low, the TOC removal operation can be temporarily suspended. Further, even when the pure water supply line is in a pure water supply operation, the maintenance of the TOC removing means can be performed.
　本発明の一態様では、ボイラブロー水の脱塩手段に由来する樹脂溶出物の影響を抑えることができる。 In one embodiment of the present invention, it is possible to suppress the influence of the resin eluate derived from the means for desalting boiler blow water.
　本発明の一態様では、ＴＯＣ除去ラインのＲＯ濃縮水がボイラブロー水の冷却水として使用される。 In one aspect of the present invention, the RO concentrated water in the TOC removal line is used as cooling water for boiler blow water.
図１は本発明の実施の形態に係るボイラ水処理装置のフロー図である。FIG. 1 is a flowchart of a boiler water treatment apparatus according to an embodiment of the present invention. 図２は別の実施の形態に係るボイラ水処理装置のフロー図である。FIG. 2 is a flowchart of a boiler water treatment apparatus according to another embodiment. 図３は比較例に係るボイラ水処理装置のフロー図である。FIG. 3 is a flowchart of the boiler water treatment apparatus according to the comparative example.
　以下、図面を参照して実施の形態について説明する。 Hereinafter, embodiments will be described with reference to the drawings.
　図１は、第１の実施の形態に係るボイラ水処理装置のフロー図である。原水としての工水（工業用水）は、前処理装置１で前処理されて純水となり、配管２を介して純水タンク３（取り出し部に相当）に導入される。純水タンク３内の純水は、ポンプ４を有する配管５を介してＩＰＰ発電装置などの発電装置６のボイラへ供給される。 FIG. 1 is a flowchart of the boiler water treatment apparatus according to the first embodiment. Industrial water (industrial water) as raw water is pretreated by the pretreatment device 1 to become pure water, and is introduced into a pure water tank 3 (corresponding to a takeout portion) via a pipe 2. Pure water in the pure water tank 3 is supplied to a boiler of a power generator 6 such as an IPP power generator via a pipe 5 having a pump 4.
　この実施の形態では、純水供給ラインは、配管２、純水タンク３、ポンプ４及び配管５を有する。発電装置６のボイラで生じたボイラブロー水は、配管７、第１熱交換器８Ｂ、冷却手段８Ａ及び配管９を有した導入ラインを介して復水脱塩装置１０に導入され、脱塩処理される。 In this embodiment, the pure water supply line has a pipe 2, a pure water tank 3, a pump 4 and a pipe 5. Boiler blow water generated in the boiler of the power generation device 6 is introduced into the condensate demineralizer 10 through the introduction line having the pipe 7, the first heat exchanger 8B, the cooling means 8A, and the pipe 9, and is desalted. The
　この実施の形態では、復水脱塩装置１０は直列に複数段（この実施の形態では２段）配置された逆浸透膜分離装置（ＲＯ装置）１１，１２と、電気脱塩装置１３とを有する。ボイラブロー水は、ＲＯ処理及び電気脱塩処理により脱塩処理されて純水となり、配管１４を介して純水タンク３に返送される。 In this embodiment, the condensate desalination apparatus 10 includes reverse osmosis membrane separation apparatuses (RO apparatuses) 11 and 12 arranged in a plurality of stages (two stages in this embodiment), and an electric desalination apparatus 13. Have. The boiler blow water is desalted by RO treatment and electric desalination treatment to become pure water, and is returned to the pure water tank 3 via the pipe 14.
　純水タンク３内の純水の一部を取り出してＴＯＣ除去処理及び脱塩処理するために、ＴＯＣ除去ラインが設けられている。純水タンク３内の純水が配管１５、第２熱交換器１６、ポンプ１７を介してＲＯ装置１８へ供給され、ＲＯ透過水が配管１９を介して純水タンク３に返送される。ＲＯ濃縮水は、配管２０を介して第１熱交換器８Ｂへ送水され、ボイラブロー水と熱交換した後、配管２１を介して前処理装置１又はそれよりも上流側の原水配管や原水タンクへ返送されるか、又は系外へ排出される。 A TOC removal line is provided in order to take out a part of pure water in the pure water tank 3 and perform TOC removal treatment and desalination treatment. Pure water in the pure water tank 3 is supplied to the RO device 18 via the pipe 15, the second heat exchanger 16, and the pump 17, and RO permeated water is returned to the pure water tank 3 via the pipe 19. The RO concentrated water is supplied to the first heat exchanger 8B via the pipe 20, and after heat exchange with the boiler blow water, the pre-treatment device 1 or upstream of the raw water pipe or the raw water tank is supplied via the pipe 21. Returned or discharged out of the system.
　第２熱交換器１６は、純水タンク３からＲＯ装置１８に供給される純水を加熱する。 The second heat exchanger 16 heats pure water supplied from the pure water tank 3 to the RO device 18.
　第１熱交換器８Ｂは、復水脱塩装置１０に送水されるボイラブロー水を冷却して降温させる。第１熱交換器８Ｂの低温流体側には、ＲＯ装置１８からの濃縮水が通水される。 The first heat exchanger 8B cools and lowers the temperature of the boiler blow water sent to the condensate demineralizer 10. The concentrated water from the RO device 18 is passed through the first heat exchanger 8B to the low temperature fluid side.
　このボイラ水処理装置にあっては、ポンプ１７を必要時に稼働させて、純水タンク３内の純水をＲＯ装置１８によってＲＯ処理することにより、純水タンク３内の純水の水質を所定範囲に維持することができる。 In this boiler water treatment apparatus, the pump 17 is operated when necessary, and the pure water in the pure water tank 3 is subjected to RO treatment by the RO device 18, whereby the quality of pure water in the pure water tank 3 is predetermined. Can be kept in range.
　ＲＯ装置１８へ供給される純水を第２熱交換器１６で加熱することにより、ＲＯ処理効率を高くすることができる。温度の高いＲＯ透過水が純水タンク３に流入することにより、純水タンク３内の水温が高くなる。 The RO treatment efficiency can be increased by heating the pure water supplied to the RO device 18 with the second heat exchanger 16. When the RO permeated water having a high temperature flows into the pure water tank 3, the water temperature in the pure water tank 3 increases.
　図１では、配管１５は取り出し部として純水タンク３に接続されているが、配管１５は純水タンク３の下流側の配管５に接続されてもよい。この場合は分岐点が取り出し部となる。 In FIG. 1, the pipe 15 is connected to the pure water tank 3 as a take-out portion, but the pipe 15 may be connected to the pipe 5 on the downstream side of the pure water tank 3. In this case, the branch point becomes the takeout part.
　図１において、第１熱交換器８Ｂを省略し、予備冷却を行わず冷却手段８Ａのみでボイラブロー水を所定温度まで冷却することも可能である。 In FIG. 1, it is possible to omit the first heat exchanger 8B and cool the boiler blow water to a predetermined temperature only by the cooling means 8A without performing preliminary cooling.
　図２は、第２の実施の形態に係るボイラ水処理装置のフロー図である。純水タンク３内の純水の水質維持用のＴＯＣ除去装置として、図１におけるＲＯ装置１８の代わりにＵＶ（紫外線）酸化装置２５とイオン交換装置２６とが設置されている。 FIG. 2 is a flowchart of the boiler water treatment apparatus according to the second embodiment. As a TOC removing device for maintaining the quality of pure water in the pure water tank 3, a UV (ultraviolet) oxidation device 25 and an ion exchange device 26 are installed instead of the RO device 18 in FIG.
　イオン交換樹脂としては、アニオン交換樹脂又は混床樹脂が好ましい。ＵＶ酸化装置（例えば、低圧ＵＶ酸化装置）２５では、ＵＶを被処理水（純水タンク３からの純水）に照射して有機物を有機酸さらにはＣＯ２まで分解する。分解により生じた有機酸、ＣＯ２等は、後段のイオン交換装置２６で除去される。イオン交換装置２６を通過した有機物濃度の低い純水が配管１９から純水タンク３に返送される。 The ion exchange resin is preferably an anion exchange resin or a mixed bed resin. UV oxidation apparatus (e.g., a low-pressure UV oxidation apparatus) decomposed at 25, the organic material by irradiating the (pure water from the pure water tank 3) the UV treated water and organic acids to CO 2. The organic acid, CO 2 and the like generated by the decomposition are removed by the ion exchange device 26 at the subsequent stage. Pure water having a low organic matter concentration that has passed through the ion exchange device 26 is returned from the pipe 19 to the pure water tank 3.
　この実施の形態では、ＲＯ装置１８は設けられていないので、ＲＯ濃縮水を第１熱交換器８Ｂへ供給するための配管２０，２１は設置されていない。第１熱交換器８Ｂの低温流体側には系外から導入した冷却水が通水される。 In this embodiment, since the RO device 18 is not provided, the pipes 20 and 21 for supplying the RO concentrated water to the first heat exchanger 8B are not installed. Cooling water introduced from outside the system is passed through the first heat exchanger 8B on the low temperature fluid side.
　発電装置６のボイラからのボイラブロー水は、配管７、第１熱交換器８Ｂ、冷却手段８Ａ及び配管９を有した導入ラインを介して復水脱塩装置１０へ送水される。その他の構成は図１と同一であり、同一符号は同一部分を示している。 Boiler blow water from the boiler of the power generation device 6 is sent to the condensate demineralizer 10 through an introduction line having the pipe 7, the first heat exchanger 8B, the cooling means 8A, and the pipe 9. Other configurations are the same as those in FIG. 1, and the same reference numerals indicate the same parts.
　図２において、第１熱交換器８Ｂを省略し、予備冷却を行わず冷却手段８Ａのみでボイラブロー水を所定温度まで冷却することも可能である。 In FIG. 2, it is also possible to omit the first heat exchanger 8B and cool the boiler blow water to a predetermined temperature only by the cooling means 8A without performing preliminary cooling.
　図１，２は本発明の一例であり、本発明は図示以外の形態とされてもよい。 1 and 2 are examples of the present invention, and the present invention may have forms other than those illustrated.
　図１，２のボイラ水処理装置の構成機器の好適例、機能等について以下に説明する。 The preferred examples and functions of the components of the boiler water treatment apparatus shown in FIGS.
１）　前処理装置１
　前処理装置１は、例えば、工業用水（市水、地下水など）等の原水に対して、凝集処理、固液分離（沈殿分離や加圧浮上分離など）、二層濾過を順次行った後に脱塩処理（カチオン交換樹脂塔、脱炭酸塔、アニオン交換樹脂塔、混床樹脂塔、電気脱塩装置などによる処理）を行うことにより、純水を製造する。 1) Pretreatment device 1
For example, the pretreatment device 1 removes the raw water such as industrial water (city water, groundwater, etc.) after performing coagulation treatment, solid-liquid separation (precipitation separation, pressurized flotation separation, etc.) and two-layer filtration sequentially. Pure water is produced by performing a salt treatment (treatment with a cation exchange resin tower, a decarboxylation tower, an anion exchange resin tower, a mixed bed resin tower, an electric desalination apparatus, or the like).
２）　純水タンク３
　純水タンク３では、前処理により製造された純水が貯留され、水質や水量の調整が行われる。 2) Pure water tank 3
In the pure water tank 3, pure water produced by the pretreatment is stored, and the water quality and the amount of water are adjusted.
３）　ＴＯＣ除去手段
　工業用水等の原水に含まれるＴＯＣ濃度が高い場合は、前処理によってＴＯＣ濃度を所定以下（例えば１００ｐｐｂ未満）まで低減することが困難となる場合がある。ＴＯＣ濃度が１００ｐｐｂ以上になるとボイラへの負担が大きくなり将来的に故障が生じる懸念がある。また、季節や気候などにより水温が変動する（例えば５～３５℃）。水温が１５℃以下になると発電用ボイラへの負担が大きくなり燃料使用量が多くなる。 3) TOC removal means When the TOC concentration contained in raw water such as industrial water is high, it may be difficult to reduce the TOC concentration to a predetermined value or less (for example, less than 100 ppb) by pretreatment. When the TOC concentration is 100 ppb or more, there is a concern that a burden on the boiler becomes large and a failure may occur in the future. In addition, the water temperature varies depending on the season and climate (for example, 5 to 35 ° C). When the water temperature is 15 ° C. or less, the load on the power generation boiler increases and the amount of fuel used increases.
　そのため、純水タンク３内の純水のＴＯＣが常に所定値以下（例えば１００ｐｐｂ以下）に維持されるように、純水供給ラインを構成する純水タンク３から分取した純水をＲＯ装置１８、又はＵＶ酸化装置２５及びイオン交換装置２６よりなるＴＯＣ除去手段でＴＯＣ除去処理を行う。 For this reason, the pure water collected from the pure water tank 3 constituting the pure water supply line is supplied to the RO device 18 so that the TOC of pure water in the pure water tank 3 is always maintained at a predetermined value or less (for example, 100 ppb or less). Alternatively, the TOC removal process is performed by the TOC removal means comprising the UV oxidation device 25 and the ion exchange device 26.
　ＴＯＣ除去手段として物理化学的手段を用いることにより、処理水に不純物が残留することを抑制できる。ＴＯＣ除去手段を、純水供給ラインから分岐したＴＯＣ除去ラインに設置することにより、例えば膜逆洗に伴う通水停止に影響されないなど、純水供給ラインと異なる制御やメンテナンスが可能となる。ＴＯＣ除去手段は既設のボイラ給水装置に、追加工事で容易に設置することができる。 By using a physicochemical means as the TOC removing means, it is possible to prevent impurities from remaining in the treated water. By installing the TOC removal means in the TOC removal line branched from the pure water supply line, for example, control and maintenance different from the pure water supply line are possible, such as being unaffected by the stoppage of water flow due to the membrane backwashing. The TOC removing means can be easily installed in an existing boiler water supply device by additional work.
　ＴＯＣ除去手段でＴＯＣ除去処理する純水の取り出し部（図１，２では純水タンク３）又はそれよりも上流側の純水供給ライン（図１，２では配管２）の純水のＴＯＣ濃度を測定するＴＯＣ濃度測定手段を設け、このＴＯＣ濃度測定手段の測定値が所定値以上のときに、ＴＯＣ除去手段によるＴＯＣ除去処理を開始するようにしてもよい。 The TOC concentration of pure water in the pure water take-off section (pure water tank 3 in FIGS. 1 and 2) or the pure water supply line (pipe 2 in FIGS. 1 and 2) upstream of the TOC removing means. TOC concentration measuring means for measuring the TOC concentration, and when the measured value of the TOC concentration measuring means is equal to or greater than a predetermined value, the TOC removal processing by the TOC removal means may be started.
　この場合、例えば、ＴＯＣ濃度測定手段とポンプ１７とを連動させて、ＴＯＣ濃度測定手段の測定値が所定値以上になったら、ポンプ１７を作動させて、ＴＯＣ除去手段に水を供給してＴＯＣ除去処理するようにしてもよい。配管１５に開閉弁を設け、この開閉弁をＴＯＣ濃度測定手段と連動させて、ＴＯＣ濃度測定手段の測定値が所定値以上のときに開閉弁を開としてＴＯＣ除去手段に純水を供給してＴＯＣ除去処理するようにしてもよい。ＴＯＣ濃度測定手段の測定値が所定値よりも低くなった場合には、ポンプ１７を停止するか開閉弁を閉としてＴＯＣ除去手段への純水の供給を停止する。 In this case, for example, the TOC concentration measuring means and the pump 17 are interlocked, and when the measured value of the TOC concentration measuring means exceeds a predetermined value, the pump 17 is operated to supply water to the TOC removing means, and the TOC. A removal process may be performed. An on-off valve is provided in the pipe 15, and this on-off valve is interlocked with the TOC concentration measuring means to open the on-off valve when the measured value of the TOC concentration measuring means is a predetermined value or more and supply pure water to the TOC removing means. You may make it perform a TOC removal process. When the measured value of the TOC concentration measuring means becomes lower than the predetermined value, the pump 17 is stopped or the on-off valve is closed to stop the supply of pure water to the TOC removing means.
　ＴＯＣ濃度測定手段の測定値に基づいて、ＴＯＣ除去手段への純水の供給の有無を制御する他、ＴＯＣ除去手段への純水の供給量を制御してもよい。例えば、ＴＯＣ濃度測定手段とポンプ１７とを連動させて、ＴＯＣ濃度測定手段の測定値が所定値以上になったら、ポンプ１７の回転数を上げて、ＴＯＣ除去手段への純水供給量を増加させ、ＴＯＣ除去処理する純水量を増やしてもよい。配管１５に流量調整弁を設け、この流量調整弁をＴＯＣ濃度測定手段と連動させて、ＴＯＣ濃度測定手段の測定値が所定値以上になったら、流量調整弁の開度を大きくしてＴＯＣ除去手段への純水供給量を増加させ、ＴＯＣ除去処理する純水量を増やしてもよい。ＴＯＣ濃度測定手段の測定値が所定値より低くなった場合には、ポンプ１７の回転数を下げるか流量調整弁の開度を小さくしてＴＯＣ除去手段への純水供給量を少なくする。 In addition to controlling whether pure water is supplied to the TOC removing means based on the measurement value of the TOC concentration measuring means, the amount of pure water supplied to the TOC removing means may be controlled. For example, by interlocking the TOC concentration measuring means and the pump 17, when the measured value of the TOC concentration measuring means exceeds a predetermined value, the rotational speed of the pump 17 is increased to increase the amount of pure water supplied to the TOC removing means. The amount of pure water to be subjected to the TOC removal process may be increased. A flow rate adjusting valve is provided in the pipe 15, and this flow rate adjusting valve is linked to the TOC concentration measuring means. When the measured value of the TOC concentration measuring means exceeds a predetermined value, the opening of the flow adjusting valve is increased to remove the TOC. The amount of pure water supplied to the means may be increased to increase the amount of pure water subjected to the TOC removal process. When the measured value of the TOC concentration measuring means becomes lower than the predetermined value, the pure water supply amount to the TOC removing means is reduced by reducing the rotational speed of the pump 17 or reducing the opening of the flow rate adjusting valve.
　ＴＯＣ濃度測定手段の測定値に基づいて、ＴＯＣ除去手段への純水の供給の有無や供給量を制御することにより、必要量の純水をＴＯＣ除去手段で処理することができ、純水のＴＯＣ除去処理に係るコストを低減することができる。 Based on the measured value of the TOC concentration measuring means, the required amount of pure water can be processed by the TOC removing means by controlling the presence or the amount of pure water supplied to the TOC removing means. Costs related to the TOC removal process can be reduced.
　ＴＯＣ除去手段への純水の供給の有無又は供給量の増減の制御は、ＴＯＣ濃度測定手段のＴＯＣ濃度の測定値が入力され、この測定値に基づいてポンプ又は弁への制御信号を出力する制御装置により、自動制御で行うことができる。 The control of whether or not the pure water is supplied to the TOC removing means or the increase / decrease in the supply amount is performed by inputting the measured value of the TOC concentration of the TOC concentration measuring means and outputting a control signal to the pump or valve based on the measured value. It can be performed automatically by the control device.
４）　発電装置６としては、高圧ボイラを備えたＩＰＰ発電装置など各種のものがある。 4) As the power generation device 6, there are various types such as an IPP power generation device equipped with a high-pressure boiler.
５）ボイラブロー水排出ライン～復水脱塩手段～復水返送ライン
　ボイラ蒸気の凝縮水は一般には高温であり（例えば７０～９７℃）、ボイラからボイラブロー水として排出された後に冷却手段８Ａ（密閉冷却塔、熱交換器など）により２０～４０℃程度に冷却された後、復水脱塩装置１０に供給される。 5) Boiler blow water discharge line to condensate demineralization means to condensate return line The boiler steam condensate is generally at a high temperature (for example, 70 to 97 ° C), and after being discharged from the boiler as boiler blow water, cooling means 8A (sealed) After cooling to about 20 to 40 ° C. by a cooling tower, a heat exchanger, etc., it is supplied to the condensate demineralizer 10.
　図１，２では、復水脱塩装置１０として、直列２段ＲＯ処理→電気脱塩を例示しているが、脱塩処理できる物理化学的手段であれば特に限定されない。 1 and 2 exemplify the two-stage RO treatment → electric desalination as the condensate desalination apparatus 10, it is not particularly limited as long as it is a physicochemical means capable of desalting.
６）　第１熱交換器８Ｂ
　図１のように、ＴＯＣ除去手段としてＲＯ装置１８を用いる場合、常温程度（５～３５℃）のＲＯ濃縮水が排出されるので、このＲＯ濃縮水を冷却手段８Ａの前段に設けられた第１熱交換器８Ｂに通水してボイラブロー水と熱交換してボイラブロー水を５０～７０℃程度に予備冷却する。これにより、復水脱塩装置１０前段に設けられた冷却手段８Ａの負荷を軽減する。 6) First heat exchanger 8B
As shown in FIG. 1, when the RO device 18 is used as the TOC removing means, the RO concentrated water at a room temperature (5 to 35 ° C.) is discharged, so this RO concentrated water is provided in the first stage of the cooling means 8A. 1 Water is passed through the heat exchanger 8B to exchange heat with the boiler blow water, and the boiler blow water is precooled to about 50 to 70 ° C. Thereby, the load of the cooling means 8A provided in the front stage of the condensate demineralizer 10 is reduced.
７）　第２熱交換器１６
　純水タンク３の水温が所定値以下（例えば１５℃以下）に低下しやすい場合は、ＴＯＣ除去手段の給水を第２熱交換器１６にて温水と熱交換して加温する。これにより、ＴＯＣ除去手段で効率的にＴＯＣ除去することが可能である。純水タンク３の水温が例えば２０～３５℃に維持されるようにすれば、ＩＰＰ発電設備の高圧ボイラの負担を軽減することができる。 7) Second heat exchanger 16
When the water temperature of the pure water tank 3 is likely to drop to a predetermined value or lower (for example, 15 ° C. or lower), the water supplied from the TOC removing unit is heated by exchanging heat with hot water in the second heat exchanger 16. Thereby, it is possible to remove the TOC efficiently by the TOC removing means. If the water temperature of the pure water tank 3 is maintained at 20 to 35 ° C., for example, the burden on the high-pressure boiler of the IPP power generation facility can be reduced.
　純水供給ライン（配管２、純水タンク３、配管５等）や、ＴＯＣ除去ライン（配管１５，１９等）中の水温を測定し、測定値が所定値以下にまで低温になったときに、第２熱交換器１６に温水を供給するように弁を切り替えて本機構による昇温を行うように制御してもよい。水温測定値に基づいて第２熱交換器１６への供給流量を調整するように流量制御してもよい。これによりボイラ給水の水温が所定範囲に維持され、ボイラへの負荷が一定範囲内に維持される。 When the water temperature in the pure water supply line (pipe 2, pure water tank 3, pipe 5, etc.) or the TOC removal line ( pipe 15, 19, etc.) is measured and the measured value is lowered to a predetermined value or lower. The valve may be switched so as to supply hot water to the second heat exchanger 16 and the temperature may be controlled by this mechanism. The flow rate may be controlled so as to adjust the supply flow rate to the second heat exchanger 16 based on the measured water temperature. Thereby, the water temperature of boiler feed water is maintained within a predetermined range, and the load on the boiler is maintained within a certain range.
［実施例１］
　千葉県工業用水（ＴＯＣ濃度２～３ｐｐｍ；水温１０℃）を図１のボイラ水処理装置によって処理し、ＩＰＰ発電装置６のボイラに給水すると共に、ボイラブロー水回収を行った。前処理装置１では、凝集処理、加圧浮上分離、二層濾過、２床３塔型イオン交換（陽イオン交換、脱炭酸、陰イオン交換）を行って純水を製造した。主な条件を下記及び表１に示す。結果を表１に示す。 [Example 1]
Chiba Prefecture industrial water (TOC concentration 2 to 3 ppm; water temperature 10 ° C.) was treated by the boiler water treatment device shown in FIG. 1 and supplied to the boiler of the IPP power generation device 6, and boiler blow water was collected. In the pretreatment apparatus 1, pure water was produced by performing agglomeration treatment, pressurized flotation separation, two-layer filtration, two-bed three-column ion exchange (cation exchange, decarboxylation, anion exchange). The main conditions are shown below and in Table 1. The results are shown in Table 1.
　　工水の平均供給量（配管２内平均流量）：３５ｍ３／ｈｒ
　　純水タンク３容積：４００ｍ３
　　ＩＰＰ発電ボイラへの平均給水量（配管５内平均流量）：３５ｍ３／ｈｒ
　　ボイラブロー水平均流量（配管７内平均流量）：１０～１２ｍ３／ｈｒ
　　ＲＯ装置１８平均給水量（配管１５内平均流量）：３４ｍ３／ｈｒ
　　ＲＯ装置１８平均透過水量（配管１９内平均流量）：３０ｍ３／ｈｒ
　　第１熱交換器８Ｂ給水平均流量：１０～１２ｍ３／ｈｒ
　　冷却手段８Ａ給水平均流量：１０～１２ｍ３／ｈｒ
　　第２熱交換器１６給水平均流量：３４ｍ３／ｈｒ Average supply amount of industrial water (average flow rate in pipe 2): 35 m 3 / hr
Pure water tank 3 volume: 400m 3
Average amount of water supply to the IPP power generation boiler (average flow rate in the pipe 5): 35 m 3 / hr
Boiler blow water average flow rate (average flow rate in pipe 7): 10 to 12 m 3 / hr
RO device 18 average water supply amount (average flow rate in pipe 15): 34 m 3 / hr
RO device 18 average permeate flow rate (average flow rate in pipe 19): 30 m 3 / hr
1st heat exchanger 8B feed water average flow rate: 10-12m 3 / hr
Cooling means 8A water supply average flow rate: 10-12 m 3 / hr
Second heat exchanger 16 average feed water flow rate: 34 m 3 / hr
［実施例２］
　ボイラ水処理装置を図２のボイラ水処理装置としたこと以外は実施例１と同一条件で運転を行った。結果を表１に示す。 [Example 2]
The operation was performed under the same conditions as in Example 1 except that the boiler water treatment apparatus shown in FIG. The results are shown in Table 1.
［実施例３］
　実施例１において、第２熱交換器１６を省略し、ＲＯ装置１８の給水の予備加熱を行わなかったこと以外は実施例１と同一条件で運転を行った。結果を表１に示す。 [Example 3]
In Example 1, the 2nd heat exchanger 16 was abbreviate | omitted, and it drive | operated on the same conditions as Example 1 except not having performed preheating of the water supply of RO apparatus 18. FIG. The results are shown in Table 1.
［実施例４］
　実施例１において、配管２０，２１、第１熱交換器８Ｂを省略し、ＲＯ濃縮水によるボイラブロー水の予備冷却を行わなかったこと以外は実施例１と同一条件で運転を行った。結果を表１に示す。 [Example 4]
In Example 1, the operation was performed under the same conditions as in Example 1 except that the pipes 20 and 21 and the first heat exchanger 8B were omitted and the boiler blow water was not preliminarily cooled with the RO concentrated water. The results are shown in Table 1.
［比較例１］
　実施例１において、ＴＯＣ除去用の配管１５、第２熱交換器１６、ポンプ１７、ＲＯ装置１８、配管１９と、配管２０，２１及び第１熱交換器８Ｂを省略し、図３のフローとしたこと以外は実施例１と同一条件で運転を行った。結果を表１に示す。 [Comparative Example 1]
In Example 1, the piping 15 for removing the TOC, the second heat exchanger 16, the pump 17, the RO device 18, the piping 19, the piping 20, 21 and the first heat exchanger 8B are omitted, and the flow of FIG. The operation was performed under the same conditions as in Example 1 except that. The results are shown in Table 1.
Figure JPOXMLDOC01-appb-T000001
Figure JPOXMLDOC01-appb-T000001
　表１の通り、実施例１～４では、比較例１に比べてボイラ給水のＴＯＣ濃度が低く、ボイラへの負荷が低減される。
　ＴＯＣ除去ラインの予備加熱を行わなかった実施例３よりも、それを行った実施例１，４の方が同じＲＯ装置におけるＴＯＣ除去率が高い。
　予備加熱を行った実施例１，２，４の方が後段のボイラへの負荷が低減される。
　同様にボイラブロー水の予備冷却を行わなかった実施例４よりも、それを行った実施例１～３の方が、後段の冷却手段への負荷が低減される。 As shown in Table 1, in Examples 1 to 4, the TOC concentration of boiler feed water is lower than that in Comparative Example 1, and the load on the boiler is reduced.
The TOC removal rate in the same RO apparatus is higher in Examples 1 and 4 in which the TOC removal line was not preheated than in Example 3 in which the TOC removal line was not preliminarily performed.
In the first, second, and fourth embodiments in which the preheating is performed, the load on the subsequent boiler is reduced.
Similarly, the load on the subsequent cooling means is reduced in the first to third embodiments in which the boiler blow water was not preliminarily cooled in the first to third embodiments.
　本発明を特定の態様を用いて詳細に説明したが、本発明の意図と範囲を離れることなく様々な変更が可能であることは当業者に明らかである。
　本出願は、２０１７年５月１２日付で出願された日本特許出願２０１７－０９５８３５に基づいており、その全体が引用により援用される。 Although the present invention has been described in detail using specific embodiments, it will be apparent to those skilled in the art that various modifications can be made without departing from the spirit and scope of the invention.
This application is based on Japanese Patent Application No. 2017-095835 filed on May 12, 2017, which is incorporated by reference in its entirety.
　１　前処理装置
　３　純水タンク
　６　発電装置
　８Ａ　冷却手段
　８Ｂ　第１熱交換器
　１０　復水脱塩装置
　１６　第２熱交換器
　１１，１２，１８　ＲＯ装置
　１３　電気脱塩装置
　２５　ＵＶ酸化装置
　２６　イオン交換装置 DESCRIPTION OF SYMBOLS 1 Pretreatment apparatus 3 Pure water tank 6 Electric power generation apparatus 8A Cooling means 8B 1st heat exchanger 10 Condensate demineralizer 16 2nd heat exchanger 11, 12, 18 RO apparatus 13 Electric desalination apparatus 25 UV oxidation apparatus 26 Ion Exchange device

Claims (10)

  1. 　原水を処理して純水を製造する前処理装置と、
    　該前処理装置からの純水をボイラへ供給する純水供給ラインと
    を有するボイラ水処理装置において、
    　該純水供給ラインから純水の一部を取り出し部から取り出してＴＯＣ除去手段でＴＯＣ除去処理し、この処理水を該取り出し部又はそれよりも上流側の該純水供給ラインに戻すＴＯＣ除去ラインを備えたことを特徴とするボイラ水処理装置。     A pretreatment device for producing raw water by treating raw water;
    In a boiler water treatment apparatus having a pure water supply line for supplying pure water from the pretreatment apparatus to the boiler,
    A TOC removal line in which a part of pure water is taken out from the take-out portion from the pure water supply line, subjected to TOC removal by the TOC removing means, and this treated water is returned to the take-out portion or the pure water supply line on the upstream side thereof. A boiler water treatment apparatus comprising:
  2. 　請求項１において、前記ＴＯＣ除去手段は、ＲＯ装置を有するか、又はＵＶ酸化装置及びイオン交換装置を有することを特徴とするボイラ水処理装置。 2. The boiler water treatment apparatus according to claim 1, wherein the TOC removing means has an RO device or a UV oxidation device and an ion exchange device.
  3. 　請求項１又は２において、前記取り出し部又はそれよりも上流側の前記純水供給ラインの純水のＴＯＣ濃度の測定手段と、
    　該測定手段の測定値が所定値以上のときに前記ＴＯＣ除去手段によるＴＯＣ除去を開始するか、又はＴＯＣ除去手段への純水供給量を増加させる純水供給量制御手段を備えたことを特徴とするボイラ水処理装置。     In Claim 1 or 2, the measuring means of the TOC concentration of the pure water of the pure water supply line upstream of the take-out portion or upstream thereof,
    A pure water supply amount control means for starting the TOC removal by the TOC removal means when the measurement value of the measurement means is equal to or greater than a predetermined value or increasing the pure water supply amount to the TOC removal means is provided. Boiler water treatment equipment.
  4. 　請求項１～３のいずれか１項において、前記ボイラからの排気蒸気が凝縮されて該ボイラから排出されたボイラブロー水を脱塩処理する復水脱塩手段と、該ボイラからのボイラブロー水を該復水脱塩手段に導入するボイラブロー水導入ラインと、該復水脱塩手段で脱塩処理された復水脱塩水を前記取り出し部又はそれよりも上流側の純水供給ラインに返送する復水脱塩水返送ラインとを備えたことを特徴とするボイラ水処理装置。 The condensate demineralizing means for demineralizing boiler blow water discharged from the boiler after the exhaust steam from the boiler is condensed, and boiler blow water from the boiler as defined in any one of claims 1 to 3 A boiler blow water introduction line to be introduced into the condensate demineralization means, and a condensate for returning the condensate demineralized water desalted by the condensate demineralization means to the take-out section or a pure water supply line upstream of the extraction section. A boiler water treatment apparatus comprising a desalted water return line.
  5. 　請求項４において、前記ＴＯＣ除去手段はＲＯ装置を有しており、
    　該ＲＯ装置のＲＯ濃縮水とボイラブロー水とを熱交換させる熱交換器を前記ボイラブロー水導入ラインに備えたことを特徴とするボイラ水処理装置。     In Claim 4, the said TOC removal means has RO apparatus,
    A boiler water treatment apparatus comprising a heat exchanger for exchanging heat between the RO concentrated water and boiler blow water of the RO apparatus in the boiler blow water introduction line.
  6. 　原水を前処理装置で処理して純水を製造し、
    　該前処理装置からの純水を純水供給ラインを経由してボイラへ供給するボイラ水処理方法において、
    　該純水供給ラインから純水の一部を取り出し部から取り出してＴＯＣ除去手段でＴＯＣ除去処理し、この処理水を該取り出し部又はそれよりも上流側の該純水供給ラインに戻すことを特徴とするボイラ水処理方法。     Raw water is treated with a pretreatment device to produce pure water,
    In a boiler water treatment method for supplying pure water from the pretreatment device to a boiler via a pure water supply line,
    A part of pure water is taken out from the take-out part from the pure water supply line and subjected to TOC removal by the TOC removing means, and the treated water is returned to the take-out part or the pure water supply line on the upstream side thereof. Boiler water treatment method.
  7. 　請求項６において、前記ＴＯＣ除去手段は、ＲＯ装置を有するか、又はＵＶ酸化装置及びイオン交換装置を有することを特徴とするボイラ水処理方法。 7. The boiler water treatment method according to claim 6, wherein the TOC removing means has an RO device, or has a UV oxidation device and an ion exchange device.
  8. 　請求項６又は７において、前記取り出し部又はそれよりも上流側の前記純水供給ラインの純水のＴＯＣ濃度を測定し、該測定値が所定値以上のときに前記ＴＯＣ除去手段によるＴＯＣ除去を開始するか、又はＴＯＣ除去手段への純水供給量を増加させることを特徴とするボイラ水処理方法。 In Claim 6 or 7, the TOC concentration of the pure water of the said extraction part or the said pure water supply line upstream from it is measured, and when this measured value is more than a predetermined value, TOC removal by the said TOC removal means is carried out. A boiler water treatment method characterized by starting or increasing the amount of pure water supplied to the TOC removing means.
  9. 　請求項６～８のいずれか１項において、前記ボイラからの排気蒸気が凝縮されて該ボイラから排出されたボイラブロー水を復水脱塩手段で脱塩処理し、該復水脱塩手段で脱塩処理された復水脱塩水を前記取り出し部又はそれよりも上流側の純水供給ラインに返送することを特徴とするボイラ水処理方法。 9. The boiler blow water discharged from the boiler according to any one of claims 6 to 8, wherein exhaust steam from the boiler is condensed and discharged from the boiler is demineralized by the condensate demineralization means, and decondensed by the condensate demineralization means. A boiler water treatment method, wherein the salt-treated condensate demineralized water is returned to the take-out section or a pure water supply line on the upstream side thereof.
  10. 　請求項９において、前記ＴＯＣ除去手段はＲＯ装置を有しており、
    　該ＲＯ装置のＲＯ濃縮水と前記復水脱塩手段に供給されるボイラブロー水とを熱交換して、該ボイラブロー水を冷却することを特徴とするボイラ水処理方法。     In Claim 9, the said TOC removal means has RO apparatus,
    A boiler water treatment method, wherein the boiler blow water is cooled by exchanging heat between the RO concentrated water of the RO device and the boiler blow water supplied to the condensate demineralization means.
PCT/JP2018/013228 2017-05-12 2018-03-29 Boiler water treatment apparatus and treatment method WO2018207492A1 (en)

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