JP2016097387A - Ammonia treatment system - Google Patents

Ammonia treatment system Download PDF

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JP2016097387A
JP2016097387A JP2014238637A JP2014238637A JP2016097387A JP 2016097387 A JP2016097387 A JP 2016097387A JP 2014238637 A JP2014238637 A JP 2014238637A JP 2014238637 A JP2014238637 A JP 2014238637A JP 2016097387 A JP2016097387 A JP 2016097387A
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Prior art keywords
boiler
drainage
line
water
hypochlorous acid
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JP2016097387A5 (en
JP6331145B2 (en
Inventor
宏幸 高波
Hiroyuki Takanami
宏幸 高波
勇作 那須
Yusaku Nasu
勇作 那須
章弘 三田村
Akihiro Mitamura
章弘 三田村
大暉 四條
Daiki SHIJO
大暉 四條
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Mitsubishi Heavy Industries Environmental and Chemical Engineering Co Ltd
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Mitsubishi Heavy Industries Environmental and Chemical Engineering Co Ltd
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Application filed by Mitsubishi Heavy Industries Environmental and Chemical Engineering Co Ltd filed Critical Mitsubishi Heavy Industries Environmental and Chemical Engineering Co Ltd
Priority to PCT/JP2015/082777 priority patent/WO2016084754A1/en
Priority to TW104138600A priority patent/TWI574921B/en
Priority to SG11201704241YA priority patent/SG11201704241YA/en
Priority to KR1020177013814A priority patent/KR101967079B1/en
Priority to CN201580063882.9A priority patent/CN107001076A/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
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • 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
    • C02F1/58—Treatment of water, waste water, or sewage by removing specified dissolved compounds
    • 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
    • C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
    • F01—MACHINES OR ENGINES IN GENERAL; ENGINE PLANTS IN GENERAL; STEAM ENGINES
    • F01K—STEAM ENGINE PLANTS; STEAM ACCUMULATORS; ENGINE PLANTS NOT OTHERWISE PROVIDED FOR; ENGINES USING SPECIAL WORKING FLUIDS OR CYCLES
    • F01K9/00—Plants characterised by condensers arranged or modified to co-operate with the engines

Abstract

PROBLEM TO BE SOLVED: To shorten the reaction time of boiler drainage with hypochlorous acid.SOLUTION: There is provided an ammonia treatment system 1 which includes: a drainage line 10 which supplies boiler drainage W to a mixing tank 9; a pH measuring device 24 which measures the pH of the boiler drainage W flowing in the drainage line 10; a pH adjusting device 23 which is provided on the drainage line 10 and adds a pH adjusting agent for adjusting the pH of the boiler drainage W to the boiler drainage W; an electrolysis device 2 which decomposes sea water or salt water with electric current to produce electrolytically treated water E having hypochlorous acid; a supply line 18 which is provided upstream from a meeting part 20 in which the supply line meets the drainage line 10 connected to the mixing tank 9 and supplies the hypochlorous acid produced by the electrolysis device 2 to the boiler drainage W; and a control device which controls the additive amount of the pH adjusting agent based on a measured value of the pH measuring device 24.SELECTED DRAWING: Figure 1

Description

本発明は、アンモニア処理システムに係り、特にボイラ設備からの排水であるボイラ排水に含まれるアンモニアを処理するアンモニア処理システムに関する。   The present invention relates to an ammonia treatment system, and more particularly, to an ammonia treatment system for treating ammonia contained in boiler wastewater that is wastewater from boiler equipment.

例えば火力発電プラントにおいて、腐食の要因となる酸素を除去するために使用されているヒドラジンは、「変位原性が認められた化学物質」と評価されていることから、近年はより安全な脱酸素剤や、脱酸素剤不使用の水処理の採用が進行している。
ヒドラジンを用いない脱酸素剤としては、水素イオン指数（ｐＨ）の値を大きくした（例えばｐＨ７〜ｐＨ１０．５）アンモニアが知られているが、脱酸素剤としてアンモニアを用いることにより今後プラントからの排水のアンモニア濃度が高くなることが想定されている（例えば非特許文献１参照）。一方、排水規制により窒素の低減も求められており、早急な対応が望まれている。 For example, hydrazine, which is used to remove oxygen that causes corrosion in thermal power plants, has been evaluated as a “chemical substance that has been recognized as a displacement source”. Adoption of water treatment without agents and oxygen scavengers is in progress.
As an oxygen scavenger that does not use hydrazine, ammonia having a large hydrogen ion index (pH) (for example, pH 7 to pH 10.5) is known. It is assumed that the ammonia concentration in the wastewater becomes high (see, for example, Non-Patent Document 1). On the other hand, reduction of nitrogen is also required by the drainage regulations, and an immediate response is desired.

特許文献１には、海水を電気分解することによって得られる次亜塩素酸ナトリウム（次亜塩素酸ソーダ）を用い、塩素処理によってアンモニアを分解するアンモニア処理システムが記載されている。このアンモニア処理システムにおいては、アンモニア含有排水であるボイラ排水が混合槽に導入されるとともに混合槽に次亜塩素酸が添加され、ボイラ排水中に存在するアンモニアと次亜塩素酸とが溶液反応して、窒素ガスまで分解される。   Patent Document 1 describes an ammonia treatment system that decomposes ammonia by chlorination using sodium hypochlorite (sodium hypochlorite) obtained by electrolyzing seawater. In this ammonia treatment system, boiler wastewater, which is ammonia-containing wastewater, is introduced into the mixing tank, and hypochlorous acid is added to the mixing tank, so that ammonia and hypochlorous acid present in the boiler wastewater react with each other. To nitrogen gas.

特開２０１４−５６３号公報JP 2014-563 A

“火力プラント水処理における脱ヒドラジンへの取組み”、[online]、三菱重工技報 Vol.46 No.2 (2009)、[平成24年3月30日検索]、インターネット<URL: http://www.mhi.co.jp/technology/review/pdf/462/462055.pdf>“Efforts to remove hydrazine in thermal power plant water treatment”, [online], Mitsubishi Heavy Industries Technical Review Vol.46 No.2 (2009), [March 30, 2012 search], Internet <URL: http: // www.mhi.co.jp/technology/review/pdf/462/462055.pdf>

ところで、特許文献１に記載のシステムにおいては、ボイラ排水と次亜塩素酸との反応時間に応じて混合槽の容量が決定される。しかしながら、ボイラ排水と次亜塩素酸との反応時間が長くなると混合槽の容量を大きくする必要があった。   By the way, in the system of patent document 1, the capacity | capacitance of a mixing tank is determined according to the reaction time of boiler waste_water | drain and hypochlorous acid. However, when the reaction time between the boiler wastewater and hypochlorous acid becomes long, it is necessary to increase the capacity of the mixing tank.

この発明は、ボイラ排水と次亜塩素酸との反応時間を短くすることができるアンモニア処理システムを提供することを目的とする。   An object of this invention is to provide the ammonia processing system which can shorten the reaction time of boiler waste_water | drain and hypochlorous acid.

本発明の第一の態様によれば、アンモニア処理システムは、ボイラ排水を混合槽へ供給する排水ラインと、前記排水ラインを流れる前記ボイラ排水のｐＨを測定するｐＨ測定装置と、前記排水ライン上に設けられ、前記ボイラ排水に前記ボイラ排水のｐＨを調整するｐＨ調整剤を添加するｐＨ調整装置と、海水又は塩水を電気分解して次亜塩素酸を有する電解処理水を生成する電解装置と、前記排水ラインと前記混合槽との合流部より上流に設けられ、前記電解装置で生成された次亜塩素酸を前記ボイラ排水に供給する供給ラインと、前記ｐＨ測定装置の測定値に基づいて前記ｐＨ調整剤の添加量を制御する制御装置と、を有することを特徴とする。   According to the first aspect of the present invention, the ammonia treatment system includes a drainage line for supplying boiler wastewater to the mixing tank, a pH measuring device for measuring the pH of the boiler wastewater flowing through the drainage line, and the drainage line. And a pH adjusting device for adding a pH adjusting agent for adjusting the pH of the boiler wastewater to the boiler wastewater, and an electrolytic device for electrolyzing seawater or salt water to generate electrolytically treated water having hypochlorous acid. Based on the measured value of the pH measuring device, a supply line that is provided upstream from the junction of the drainage line and the mixing tank and that supplies hypochlorous acid generated by the electrolysis device to the boiler drainage And a control device for controlling the amount of the pH adjuster added.

このような構成によれば、ｐＨ調整剤を添加してボイラ排水のｐＨを調整することにより、ボイラ排水と次亜塩素酸との反応時間を短くすることができる。   According to such a structure, the reaction time of boiler wastewater and hypochlorous acid can be shortened by adding a pH adjuster and adjusting the pH of boiler wastewater.

上記アンモニア処理システムにおいて、前記ｐＨ測定装置は、前記ｐＨ調整装置の下流側であって、前記ｐＨ調整装置によって添加された前記ｐＨ調整剤によって調整された前記ボイラ排水のｐＨが安定する位置に配置されてもよい。   In the ammonia treatment system, the pH measuring device is disposed downstream of the pH adjusting device and at a position where the pH of the boiler wastewater adjusted by the pH adjusting agent added by the pH adjusting device is stable. May be.

このような構成によれば、ｐＨ測定装置によって、より正確なボイラ排水のｐＨを測定することができる。これにより、ｐＨ調整装置によるボイラ排水のｐＨの調整を正確に行うことができる。   According to such a configuration, the pH of the boiler wastewater can be measured more accurately by the pH measuring device. Thereby, adjustment of pH of boiler drainage by a pH adjustment device can be performed correctly.

上記アンモニア処理システムにおいて、前記排水ラインの上流側に設けられて前記ボイラ排水を貯留する貯留槽と、前記貯留槽に貯留された前記ボイラ排水のｐＨを測定する貯留槽ｐＨ測定装置と、を有し、前記制御装置は、前記貯留槽ｐＨ測定装置の測定値に基づいて前記電解装置にて生成される次亜塩素酸量を制御してもよい。   The ammonia treatment system includes a storage tank that is provided upstream of the drainage line and stores the boiler drainage, and a storage tank pH measurement device that measures the pH of the boiler drainage stored in the storage tank. And the said control apparatus may control the amount of hypochlorous acid produced | generated in the said electrolysis apparatus based on the measured value of the said storage tank pH measurement apparatus.

本発明によれば、ｐＨ調整剤を添加してボイラ排水のｐＨを調整することにより、ボイラ排水と次亜塩素酸との反応時間を短くすることができる。   According to the present invention, the reaction time between boiler wastewater and hypochlorous acid can be shortened by adding a pH adjuster to adjust the pH of the boiler wastewater.

本発明の第一実施形態のアンモニア処理システムの概略構成図である。It is a schematic block diagram of the ammonia processing system of 1st embodiment of this invention. 本発明の第一実施形態のアンモニア処理システムの混合槽におけるアンモニア分解速度とボイラ排水のｐＨとの関係を示すグラフである。It is a graph which shows the relationship between the ammonia decomposition rate in the mixing tank of the ammonia treatment system of 1st embodiment of this invention, and the pH of boiler waste_water | drain. 本発明の第二実施形態のアンモニア処理システムの概略構成図である。It is a schematic block diagram of the ammonia processing system of 2nd embodiment of this invention.

（第一実施形態）
以下、本発明の第一実施形態のアンモニア処理システム１について図面を参照して詳細に説明する。
図１は、本発明の第一実施形態のアンモニア処理システム１を有するプラントＰの概略構成図である。図１に示すように、アンモニア処理システム１は、排熱回収ボイラＢを備えたコンバインドサイクル発電プラントＰから排出されるボイラ排水Ｗを処理するためのシステムである。 (First embodiment)
Hereinafter, the ammonia processing system 1 of 1st embodiment of this invention is demonstrated in detail with reference to drawings.
FIG. 1 is a schematic configuration diagram of a plant P having an ammonia treatment system 1 according to the first embodiment of the present invention. As shown in FIG. 1, the ammonia treatment system 1 is a system for treating boiler waste water W discharged from a combined cycle power plant P having an exhaust heat recovery boiler B.

アンモニア処理システム１は、海水電解装置２と、制御装置（図示せず）と、を主な構成要素として備えている。
コンバインドサイクル発電プラントＰ（以下、プラントＰと呼ぶ）は、ガスタービン（図示せず）と、ガスタービンからの排気ガスが送られる排熱回収ボイラＢ（以下、ボイラＢと呼ぶ）と、蒸気タービン（図示せず）と、ガスタービンと蒸気タービンの回転駆動力により駆動されて発電する発電機（図示せず）と、を有する構成とすることができる。 The ammonia treatment system 1 includes a seawater electrolysis device 2 and a control device (not shown) as main components.
A combined cycle power plant P (hereinafter referred to as plant P) includes a gas turbine (not shown), an exhaust heat recovery boiler B (hereinafter referred to as boiler B) to which exhaust gas from the gas turbine is sent, and a steam turbine. (Not shown) and a generator (not shown) that generates electric power by being driven by the rotational driving force of the gas turbine and the steam turbine.

プラントＰには海水の取水口３から第一海水供給ライン４を介して取水された海水Ｍが導入されて、例えば冷却などの用途に使用される。第一海水供給ライン４には、海水Ｍを送水する海水供給ポンプ（図示せず）、及び海水Ｍの流量を調整する海水流量調整バルブ（図示せず）が設けられている。
例えばボイラＢのボイラ水には、腐食の要因となる酸素を除去するための脱酸素剤としてアンモニアが使用されている。よって、ボイラＢから排出されるボイラ排水Ｗは、アンモニア（ＮＨ３）、アンモニウムイオン（ＮＨ４ ＋）等のアンモニア性窒素を含むアンモニア性窒素含有排水である。 Seawater M taken from the seawater intake 3 through the first seawater supply line 4 is introduced into the plant P, and used for applications such as cooling. The first seawater supply line 4 is provided with a seawater supply pump (not shown) that supplies the seawater M and a seawater flow rate adjustment valve (not shown) that adjusts the flow rate of the seawater M.
For example, in the boiler water of boiler B, ammonia is used as an oxygen scavenger for removing oxygen that causes corrosion. Therefore, the boiler waste water W discharged from the boiler B is an ammonia nitrogen-containing waste water containing ammonia nitrogen such as ammonia (NH 3 ) and ammonium ions (NH 4 + ).

ボイラＢから排出されたボイラ排水Ｗは、貯留槽５に貯留される。貯留槽５には、ボイラ排水Ｗを減温するための減温希釈水（工業用水道）を貯留槽５に投入するための希釈水導入装置６が設けられている。貯留槽５内の処理水は、処理水の温度を計測可能な温度計（図示せず）によって計測された温度に基づいて、所定の温度以下に管理されている。また、貯留槽５には、貯留槽５内の処理水のｐＨ（水素イオン指数）を計測する貯留槽ｐＨ測定装置７が設けられている。   The boiler waste water W discharged from the boiler B is stored in the storage tank 5. The storage tank 5 is provided with a dilution water introducing device 6 for introducing a temperature-reduced diluted water (industrial water supply) for reducing the temperature of the boiler waste water W into the storage tank 5. The treated water in the storage tank 5 is managed below a predetermined temperature based on the temperature measured by a thermometer (not shown) that can measure the temperature of the treated water. In addition, the storage tank 5 is provided with a storage tank pH measurement device 7 that measures the pH (hydrogen ion index) of the treated water in the storage tank 5.

貯留槽５の下流側には、混合槽９が設けられている。貯留槽５と混合槽９とは排水ライン１０を介して接続されている。即ち、貯留槽５に貯留され、減温されたボイラ排水Ｗは、排水ライン１０を介して混合槽９に導入された後放流される。排水ライン１０には、貯留槽５に貯留されているボイラ排水Ｗを混合槽９に送水する排水供給ポンプ１６が設けられている。   A mixing tank 9 is provided on the downstream side of the storage tank 5. The storage tank 5 and the mixing tank 9 are connected via a drainage line 10. That is, the boiler waste water W stored in the storage tank 5 and reduced in temperature is introduced into the mixing tank 9 through the drain line 10 and then discharged. The drainage line 10 is provided with a drainage supply pump 16 that feeds the boiler drainage W stored in the storage tank 5 to the mixing tank 9.

海水電解装置２は、第二海水供給ライン１１を介して取水口３から導入された海水Ｍの電気分解を行う装置である。第二海水供給ライン１１には、海水Ｍを送水する海水供給ポンプ１４、及び海水Ｍの流量を調整する海水流量調整バルブ１５が設けられている。
海水電解装置２は、電解槽１２と、直流電源装置１３と、を有している。海水電解装置２は、海水Ｍを電気分解することによって、次亜塩素酸ナトリウム（塩素、次亜塩素酸ソーダ）を含む電解処理水Ｅを生成する装置である。電解槽１２は、複数の電極（図示せず）を有している。 The seawater electrolysis apparatus 2 is an apparatus that performs electrolysis of the seawater M introduced from the water intake 3 through the second seawater supply line 11. The second seawater supply line 11 is provided with a seawater supply pump 14 that supplies the seawater M and a seawater flow rate adjustment valve 15 that adjusts the flow rate of the seawater M.
The seawater electrolysis apparatus 2 includes an electrolytic cell 12 and a DC power supply device 13. The seawater electrolysis apparatus 2 is an apparatus that generates electrolyzed water E containing sodium hypochlorite (chlorine, sodium hypochlorite) by electrolyzing seawater M. The electrolytic cell 12 has a plurality of electrodes (not shown).

直流電源装置１３は、海水Ｍの電気分解に供される電流を供給する装置であって、例えば、直流電源と定電流制御回路とを備える構成を採用することができる。直流電源は、直流電力を出力する電源であって、例えば交流電源から出力される交流電力を直流に整流して出力する構成であってもよい。   The DC power supply device 13 is a device that supplies a current to be used for electrolysis of the seawater M. For example, a configuration including a DC power supply and a constant current control circuit can be employed. The DC power source is a power source that outputs DC power, and may be configured to rectify and output AC power output from the AC power source to DC, for example.

本実施形態の海水電解装置２は、海水Ｍを電解槽１２に一回のみ通すワンスルー方式である。海水電解装置２としては、上記ワンスルー方式の他に、電解槽１２の下流側（電解槽１２の流出口）と電解槽１２の上流側（電解槽１２の流入口）とを循環流路によって接続して、海水を循環させるリサイクル方式を採用してもよい。即ち、海水電解装置２は、海水Ｍを用いて次亜塩素酸を生成することができれば、どのような形式のものでもよい。   The seawater electrolysis apparatus 2 of the present embodiment is a one-through system in which the seawater M is passed through the electrolytic cell 12 only once. As the seawater electrolysis apparatus 2, in addition to the one-through method, the downstream side of the electrolytic cell 12 (outlet of the electrolytic cell 12) and the upstream side of the electrolytic cell 12 (inlet of the electrolytic cell 12) are connected by a circulation channel. Then, a recycling method for circulating seawater may be adopted. That is, the seawater electrolysis apparatus 2 may be of any type as long as it can generate hypochlorous acid using the seawater M.

海水電解装置２にて生成された電解処理水Ｅは、供給ライン１８を介して混合槽９に導入されて、ボイラ排水Ｗと混合される。
また、排水ライン１０上であって、供給ライン１８との合流部２０よりも下流側（混合槽９側）には、ボイラ排水Ｗと電解処理水Ｅとの混合を促進するラインミキサ２１が設けられている。 The electrolyzed water E generated in the seawater electrolyzer 2 is introduced into the mixing tank 9 via the supply line 18 and mixed with the boiler waste water W.
A line mixer 21 that promotes the mixing of the boiler waste water W and the electrolytically treated water E is provided on the drain line 10 and downstream of the junction 20 with the supply line 18 (on the mixing tank 9 side). It has been.

混合槽９には、ボイラ排水Ｗと電解処理水Ｅが導入されて、ボイラ排水Ｗ中に存在するアンモニアと次亜塩素酸とが溶液反応して窒素ガス（Ｎ２）まで分解される。即ち、混合槽９において、アンモニアが処理されて、ボイラ排水Ｗは放流可能な状態となる。 Boiler waste water W and electrolytically treated water E are introduced into the mixing tank 9, and ammonia and hypochlorous acid present in the boiler waste water W undergo a solution reaction and are decomposed to nitrogen gas (N 2 ). That is, in the mixing tank 9, ammonia is processed and the boiler waste water W is in a state where it can be discharged.

本実施形態の排水ライン１０上には、上流側より順に排水ライン１０を流れるボイラ排水ＷのｐＨ（水素イオン指数）を調整するｐＨ調整装置２３と、ボイラ排水ＷのｐＨを測定するｐＨ測定装置２４が設けられている。ｐＨ調整装置２３とｐＨ測定装置２４は、排水ライン１０と供給ライン１８の合流部２０よりも上流側に設けられている。即ち、ｐＨ測定装置２４は、ｐＨ調整装置２３の下流側に設けられ、ｐＨ測定装置２４の下流側にて電解処理水Ｅが混合される。   On the drainage line 10 of the present embodiment, a pH adjusting device 23 that adjusts the pH (hydrogen ion index) of the boiler drainage W that flows through the drainage line 10 in order from the upstream side, and a pH measurement device that measures the pH of the boiler drainage W. 24 is provided. The pH adjusting device 23 and the pH measuring device 24 are provided on the upstream side of the junction 20 of the drain line 10 and the supply line 18. That is, the pH measuring device 24 is provided on the downstream side of the pH adjusting device 23, and the electrolytically treated water E is mixed on the downstream side of the pH measuring device 24.

ｐＨ調整装置２３は、排水ライン１０を流れるボイラ排水ＷにｐＨ調整剤を添加してボイラ排水ＷのｐＨを調整する装置である。ｐＨ調整剤は、塩酸などの酸又はアルカリ剤が用いられる。本実施形態のボイラ排水Ｗは、アルカリ性側である場合が多く、主として塩酸が添加される。   The pH adjusting device 23 is a device that adjusts the pH of the boiler drainage W by adding a pH adjuster to the boiler drainage W flowing through the drainage line 10. An acid or alkali agent such as hydrochloric acid is used as the pH adjuster. The boiler waste water W of the present embodiment is often on the alkaline side, and hydrochloric acid is mainly added.

ｐＨ測定装置２４は、ｐＨ調整装置２３よりも十分下流側に設置されている。具体的には、ｐＨ測定装置２４は、ｐＨ調整装置２３によって添加されたｐＨ調整剤がボイラ排水Ｗと混合され、適切に反応した後のボイラ排水ＷのｐＨを測定できる位置に配置されている。換言すれば、ｐＨ測定装置２４は、ｐＨ調整装置２３によって添加されたｐＨ調整剤によって調整されたボイラ排水ＷのｐＨが安定する位置に配置されている。   The pH measuring device 24 is installed sufficiently downstream of the pH adjusting device 23. Specifically, the pH measuring device 24 is arranged at a position where the pH adjusting agent added by the pH adjusting device 23 can be mixed with the boiler waste water W and can measure the pH of the boiler waste water W after reacting appropriately. . In other words, the pH measuring device 24 is disposed at a position where the pH of the boiler waste water W adjusted by the pH adjusting agent added by the pH adjusting device 23 is stabilized.

ここで、混合槽９におけるアンモニア分解速度とボイラ排水ＷのｐＨとの関係について説明する。発明者らの調査によれば、混合槽９におけるアンモニア分解速度とボイラ排水ＷのｐＨとの関係は、図２に示すようになる。図２に示すように、ボイラ排水ＷのｐＨを８．５前後とした場合、混合槽９におけるアンモニアの分解速度が向上することがわかった。
この関係に基づき、制御装置は、ｐＨ測定装置２４の測定値、即ち排水ライン１０の合流部２０よりも上流側のボイラ排水ＷのｐＨがｐＨ＝７．５〜９．５となるように、ｐＨ調整装置２３を制御してｐＨ調整剤の添加量を調整する。例えば、制御装置は、ボイラ排水ＷのｐＨが１０（アルカリ側）であった場合、ボイラ排水Ｗに塩酸を添加するようにｐＨ調整装置２３を制御する。 Here, the relationship between the ammonia decomposition rate in the mixing tank 9 and the pH of the boiler waste water W will be described. According to the inventors' investigation, the relationship between the ammonia decomposition rate in the mixing tank 9 and the pH of the boiler waste water W is as shown in FIG. As shown in FIG. 2, when the pH of the boiler waste water W was set to around 8.5, it turned out that the decomposition | disassembly rate of ammonia in the mixing tank 9 improves.
Based on this relationship, the control device is configured so that the measured value of the pH measuring device 24, that is, the pH of the boiler waste water W upstream of the merging portion 20 of the drain line 10 becomes pH = 7.5 to 9.5. The pH adjusting device 23 is controlled to adjust the addition amount of the pH adjusting agent. For example, when the pH of the boiler waste water W is 10 (alkali side), the control device controls the pH adjusting device 23 so that hydrochloric acid is added to the boiler waste water W.

次に、本実施形態のアンモニア処理システム１の作用について説明する。
まず、ボイラＢから排出されたボイラ排水Ｗは、貯留槽５に貯留される。本実施形態のボイラ排水ＷのｐＨは、１０．５前後であり、アルカリ性を示している。ボイラ排水Ｗと同時に、減温希釈水が貯留槽５に投入される。これにより、貯留槽５内のボイラ排水ＷのｐＨは例えば９．９となる。貯留槽５に貯留されたボイラ排水Ｗは、排水供給ポンプ１６を用いて所定速度で排水ライン１０に送水される。 Next, the operation of the ammonia processing system 1 of the present embodiment will be described.
First, the boiler waste water W discharged from the boiler B is stored in the storage tank 5. The pH of the boiler waste water W of this embodiment is around 10.5, indicating alkalinity. Simultaneously with the boiler waste water W, the temperature-reduced diluted water is introduced into the storage tank 5. Thereby, the pH of the boiler waste water W in the storage tank 5 becomes 9.9, for example. The boiler waste water W stored in the storage tank 5 is fed to the drain line 10 at a predetermined speed using the drain supply pump 16.

制御装置は、ｐＨ測定装置２４にて測定されたｐＨに基づいて、ｐＨ調整装置２３を用いてボイラ排水ＷにｐＨ調整剤を投入する。制御装置は、ボイラ排水ＷのｐＨが７．５〜９．５となるように、ｐＨ調整装置２３の制御を行う。   Based on the pH measured by the pH measuring device 24, the control device feeds the pH adjusting agent into the boiler waste water W using the pH adjusting device 23. The control device controls the pH adjusting device 23 so that the pH of the boiler waste water W becomes 7.5 to 9.5.

一方、制御装置は、貯留槽ｐＨ測定装置７によって測定されるボイラ排水ＷのｐＨに基づいて必要な次亜塩素酸量を算出し、直流電源装置１３の出力電流値を決定する。そして、混合槽９における処理時間などから必要とされる電解処理水量Ｅを決定する。   On the other hand, the control device calculates the amount of hypochlorous acid required based on the pH of the boiler waste water W measured by the storage tank pH measurement device 7 and determines the output current value of the DC power supply device 13. And the amount E of electrolytic treatment water required from the processing time etc. in the mixing tank 9 is determined.

貯留槽ｐＨ測定装置７によって測定されるボイラ排水ＷのｐＨとアンモニア性窒素濃度は相関性があるので、ボイラ排水ＷのｐＨを測定することによって貯留槽５内の窒素濃度が解る。アンモニア性窒素濃度に対する次亜塩素酸量も相関性があり、次亜塩素酸量は直流電源装置１３の電流値に対して比例して増減する。よって、貯留槽５内のボイラ排水ＷのｐＨを測定することで直流電源装置１３を制御し、次亜塩素酸の生成量（アンモニア性窒素除去量）を決定することが可能となる。   Since the pH of the boiler waste water W measured by the storage tank pH measurement device 7 and the ammonia nitrogen concentration are correlated, the nitrogen concentration in the storage tank 5 can be determined by measuring the pH of the boiler waste water W. The amount of hypochlorous acid with respect to the ammoniacal nitrogen concentration is also correlated, and the amount of hypochlorous acid increases or decreases in proportion to the current value of the DC power supply device 13. Therefore, it is possible to control the DC power supply 13 by measuring the pH of the boiler waste water W in the storage tank 5 and determine the amount of hypochlorous acid produced (ammonia nitrogen removal amount).

上記実施形態によれば、アンモニア性窒素を含む排水であるボイラ排水Ｗに次亜塩素酸を含む電解処理水Ｅが添加されることによって、ボイラ排水Ｗに含まれるアンモニアを分解処理することができる。   According to the said embodiment, the ammonia contained in the boiler waste water W can be decomposed | disassembled by adding the electrolytically treated water E containing hypochlorous acid to the boiler waste water W which is a waste water containing ammonia nitrogen. .

また、ｐＨ調整剤を添加してボイラ排水ＷのｐＨを調整することにより、ボイラ排水Ｗと次亜塩素酸との反応時間を短くすることができる。特に、ｐＨを７．５〜９．５の範囲に調整することにより、ボイラ排水Ｗと次亜塩素酸との反応時間をより短くすることができる。   Moreover, the reaction time of the boiler waste water W and hypochlorous acid can be shortened by adding the pH adjuster and adjusting the pH of the boiler waste water W. In particular, the reaction time between the boiler waste water W and hypochlorous acid can be further shortened by adjusting the pH to a range of 7.5 to 9.5.

また、ボイラ排水Ｗに添加されるｐＨ調整剤が電解処理水Ｅが供給される合流部２０よりも上流側にて添加されることによって、電解処理水ＥによるｐＨ変動の影響を受けることなく、ボイラ排水ＷのｐＨを調整することができる。
また、貯留槽５内のボイラ排水ＷのｐＨを測定することによって、直流電源装置１３を制御し、次亜塩素酸の生成量を決定することが可能となる。 In addition, the pH adjuster added to the boiler waste water W is added on the upstream side of the junction 20 to which the electrolytically treated water E is supplied, so that the pH is not affected by the electrolytically treated water E. The pH of the boiler waste water W can be adjusted.
In addition, by measuring the pH of the boiler waste water W in the storage tank 5, it is possible to control the DC power supply device 13 and determine the amount of hypochlorous acid produced.

（第二実施形態）
以下、本発明の第二実施形態のアンモニア処理システム１Ｂを図面に基づいて説明する。なお、本実施形態では、上述した第一実施形態との相違点を中心に述べ、同様の部分についてはその説明を省略する。 (Second embodiment)
Hereinafter, the ammonia processing system 1B of 2nd embodiment of this invention is demonstrated based on drawing. In the present embodiment, differences from the first embodiment described above will be mainly described, and description of similar parts will be omitted.

図２に示すように、本実施形態のアンモニア処理システム１Ｂは、海水電解装置２にて生成された電解処理水Ｅを取水口３に注入する注入ライン１７を有している。電解処理水Ｅ（次亜塩素酸ナトリウム）が取水口３に注入されることによって、取水口３に対する海洋生物の付着を抑制することができる。即ち、本実施形態の海水電解装置２は、海洋生物付着防止装置としての機能を有する。   As shown in FIG. 2, the ammonia treatment system 1 </ b> B of the present embodiment has an injection line 17 for injecting the electrolytically treated water E generated by the seawater electrolyzer 2 into the water inlet 3. By injecting the electrolyzed water E (sodium hypochlorite) into the water intake 3, adhesion of marine organisms to the water intake 3 can be suppressed. That is, the seawater electrolysis apparatus 2 of this embodiment has a function as a marine organism adhesion prevention apparatus.

海水電解装置２と取水口３とを接続する注入ライン１７からは、電解処理水Ｅを混合槽９に供給する供給ライン１８が分岐している。即ち、海水電解装置２にて生成された電解処理水Ｅは、注入ライン１７から分岐する供給ライン１８を介して混合槽９に導入されて、ボイラ排水Ｗと混合される。供給ライン１８には、電解処理水Ｅの流量を調整する流量調整バルブ１９が設けられている。   A supply line 18 for supplying the electrolyzed water E to the mixing tank 9 is branched from an injection line 17 that connects the seawater electrolysis apparatus 2 and the water intake 3. That is, the electrolytically treated water E generated by the seawater electrolyzer 2 is introduced into the mixing tank 9 through the supply line 18 branched from the injection line 17 and mixed with the boiler waste water W. The supply line 18 is provided with a flow rate adjusting valve 19 that adjusts the flow rate of the electrolytically treated water E.

制御装置は、流量調整バルブ１９を調整することによって、注入ライン１７から注入される電解処理水Ｅ（次亜塩素酸ナトリウム）の量を制御する。第一実施形態の制御装置と同様に、制御装置は、貯留槽ｐＨ測定装置７によって測定されるボイラ排水ＷのｐＨに基づいて必要な次亜塩素酸量を算出し、直流電源装置１３の出力電流値を決定する。そして、混合槽９における処理時間などから必要とされる電解処理水量Ｅを決定する。   The control device controls the amount of electrolytically treated water E (sodium hypochlorite) injected from the injection line 17 by adjusting the flow rate adjusting valve 19. Similar to the control device of the first embodiment, the control device calculates the amount of hypochlorous acid required based on the pH of the boiler waste water W measured by the storage tank pH measurement device 7, and outputs the DC power supply 13. Determine the current value. And the amount E of electrolytic treatment water required from the processing time etc. in the mixing tank 9 is determined.

また、海水電解装置２にて生成された電解処理水Ｅは、注入ライン１７を介して海水Ｍの取水口３に注入される。電解処理水Ｅが取水口３に注入されることによって、取水口３に対する海洋生物の付着を抑制することができる。   Further, the electrolytically treated water E generated by the seawater electrolysis apparatus 2 is injected into the water intake 3 of the seawater M through the injection line 17. By injecting the electrolyzed water E into the water intake 3, adhesion of marine organisms to the water intake 3 can be suppressed.

なお、本発明の技術範囲は上記各実施形態に限定されるものではなく、本発明の趣旨を逸脱しない範囲において、種々の変更を加えることが可能である。
例えば、上記実施形態の電解処理水Ｅの供給ライン１８は、ボイラ排水Ｗが流れる排水ライン１０に接続されているが、供給ライン１８を直接混合槽９に接続してもよい。
例えば、上記実施形態では、海水電解装置２には海水Ｍが導入される構成を示したが、海水電解装置２に塩水を導入する構成としてもよい。即ち、海水電解装置２に導入される液体は、海水Ｍと同様に塩素イオン（Ｃｌ−）を含んでいればよい。
また、混合槽９又は混合槽９の下流にｐＨ、残留塩素、水質などを測定する手段を設けて、廃水が基準に満たない場合に、廃水を貯留槽５に戻すラインを設けてもよい。 The technical scope of the present invention is not limited to the above-described embodiments, and various modifications can be made without departing from the spirit of the present invention.
For example, the supply line 18 of the electrolytically treated water E according to the above embodiment is connected to the drainage line 10 through which the boiler drainage W flows, but the supply line 18 may be directly connected to the mixing tank 9.
For example, in the above-described embodiment, the configuration in which the seawater M is introduced into the seawater electrolysis apparatus 2 is described, but the configuration in which saltwater is introduced into the seawater electrolysis apparatus 2 may be employed. That is, the liquid introduced into the seawater electrolysis apparatus 2 only needs to contain chlorine ions (Cl − ) like the seawater M.
In addition, a means for measuring pH, residual chlorine, water quality, etc. may be provided downstream of the mixing tank 9 or the mixing tank 9, and a line for returning the waste water to the storage tank 5 when the waste water does not meet the standard may be provided.

１，１Ｂ アンモニア処理システム
２ 海水電解装置（電解装置）
３ 取水口
４ 第一海水供給ライン
５ 貯留槽
６ 希釈水導入装置
７ 貯留槽ｐＨ測定装置
９ 混合槽
１０ 排水ライン
１１ 第二海水供給ライン
１２ 電解槽
１３ 直流電源装置
１４ 海水供給ポンプ
１５ 海水流量調整バルブ
１６ 排水供給ポンプ
１７ 注入ライン
１８ 供給ライン
１９ 流量調整バルブ
２０ 合流部
２１ ラインミキサ
２３ ｐＨ調整装置
２４ ｐＨ測定装置
Ｂ ボイラ
Ｅ 電解処理水
Ｍ 海水
Ｐ プラント
Ｗ ボイラ排水 1,1B Ammonia treatment system 2 Seawater electrolyzer (electrolyzer)
DESCRIPTION OF SYMBOLS 3 Intake port 4 1st seawater supply line 5 Reservoir 6 Dilution water introduction device 7 Reservoir pH measurement device 9 Mixing tank 10 Drainage line 11 Second seawater supply line 12 Electrolyzer 13 DC power supply device 14 Seawater supply pump 15 Seawater flow rate adjustment Valve 16 Drainage supply pump 17 Injection line 18 Supply line 19 Flow rate adjustment valve 20 Junction part 21 Line mixer 23 pH adjustment device 24 pH measurement device B Boiler E Electrolyzed water M Seawater P Plant W Boiler drainage

Claims (3)

ボイラ排水を混合槽へ供給する排水ラインと、
前記排水ラインを流れる前記ボイラ排水のｐＨを測定するｐＨ測定装置と、
前記排水ライン上に設けられ、前記ボイラ排水に前記ボイラ排水のｐＨを調整するｐＨ調整剤を添加するｐＨ調整装置と、
海水又は塩水を電気分解して次亜塩素酸を有する電解処理水を生成する電解装置と、
前記排水ラインと前記混合槽との合流部より上流に設けられ、前記電解装置で生成された次亜塩素酸を前記ボイラ排水に供給する供給ラインと、
前記ｐＨ測定装置の測定値に基づいて前記ｐＨ調整剤の添加量を制御する制御装置と、を有するアンモニア処理システム。 A drainage line for supplying boiler wastewater to the mixing tank;
A pH measuring device for measuring the pH of the boiler drainage flowing through the drainage line;
A pH adjusting device which is provided on the drainage line and adds a pH adjusting agent for adjusting the pH of the boiler drainage to the boiler drainage;
An electrolyzer that electrolyzes seawater or salt water to produce electrolytically treated water having hypochlorous acid;
A supply line that is provided upstream from a junction between the drainage line and the mixing tank, and supplies hypochlorous acid generated by the electrolysis device to the boiler drainage;
And a control device that controls the amount of the pH adjuster added based on the measured value of the pH measuring device. 前記ｐＨ測定装置は、前記ｐＨ調整装置の下流側であって、前記ｐＨ調整装置によって添加された前記ｐＨ調整剤によって調整された前記ボイラ排水のｐＨが安定する位置に配置されている請求項１に記載のアンモニア処理システム。   The said pH measurement apparatus is arrange | positioned in the position where the pH of the said boiler waste_water | drain adjusted with the said pH adjuster added by the said pH adjuster is stabilized downstream of the said pH adjuster. Ammonia treatment system as described in 1. 前記排水ラインの上流側に設けられて前記ボイラ排水を貯留する貯留槽と、
前記貯留槽に貯留された前記ボイラ排水のｐＨを測定する貯留槽ｐＨ測定装置と、を有し、
前記制御装置は、前記貯留槽ｐＨ測定装置の測定値に基づいて前記電解装置にて生成される次亜塩素酸量を制御する請求項１又は請求項２に記載のアンモニア処理システム。 A storage tank that is provided upstream of the drainage line and stores the boiler drainage;
A storage tank pH measurement device for measuring the pH of the boiler wastewater stored in the storage tank,
The ammonia processing system according to claim 1 or 2, wherein the control device controls an amount of hypochlorous acid generated in the electrolysis device based on a measurement value of the storage tank pH measurement device.
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