JP2002172384A - Method for treating waste water containing ammonia and hydrogen peroxide - Google Patents
Method for treating waste water containing ammonia and hydrogen peroxideInfo
- Publication number
- JP2002172384A JP2002172384A JP2000370316A JP2000370316A JP2002172384A JP 2002172384 A JP2002172384 A JP 2002172384A JP 2000370316 A JP2000370316 A JP 2000370316A JP 2000370316 A JP2000370316 A JP 2000370316A JP 2002172384 A JP2002172384 A JP 2002172384A
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- Prior art keywords
- hydrogen peroxide
- ammonia
- wastewater
- stripping tower
- containing ammonia
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、アンモニアと過酸
化水素を含む排水の処理方法に関する。さらに詳しく
は、本発明は、排水中に含まれるアンモニアと過酸化水
素を、簡単な単位装置を用いて、効率よく同時に除去す
ることができるアンモニアと過酸化水素を含む排水の処
理方法に関する。[0001] The present invention relates to a method for treating wastewater containing ammonia and hydrogen peroxide. More specifically, the present invention relates to a method for treating wastewater containing ammonia and hydrogen peroxide, which can efficiently and simultaneously remove ammonia and hydrogen peroxide contained in the wastewater using a simple unit device.
【０００２】[0002]
【従来の技術】半導体の製造プロセスからは、アンモニ
アと過酸化水素を含む排水が排出される。排水中のアン
モニアは、河川、湖沼などの閉鎖性水域においては富栄
養化の原因となるので、除去する必要がある。また、過
酸化水素は、ＣＯＤMnの値を高めるので、分解する必要
がある。従来、アンモニアと過酸化水素を含む排水は、
過酸化水素を亜硫酸水素ナトリウムなどによる還元処理
又は活性炭との接触などによる分解処理を行ったのち、
アンモニアを生物硝化脱窒処理により除去していた。し
かし、薬剤の添加や活性炭との接触による過酸化水素の
分解は、制御がむつかしく、排水中の過酸化水素の濃度
の変動に対して、安定した分解処理を行うことが困難で
ある。また、生物処理によるアンモニアの除去には、汚
泥が発生する、維持管理が容易でない、反応速度が遅い
ので、広い装置設置面積を必要とするなどの問題があ
る。このような問題を解決し、排水中の過酸化水素とア
ンモニアを同時に分解する方法として、本出願人は、先
に、特開平５−２６９４７５号公報において、過酸化水
素とアンモニアを含む排水を８０〜１７０℃において、
酸化還元触媒と接触させる方法を提案した。この方法に
よると、一工程で処理することができ、汚泥の発生もな
く、水質の制御も容易であるが、高温、高圧での操作が
必要であり、設備費が高いという問題がある。本出願人
は、また、特開２０００−５１８７１号公報において、
排水中の過酸化水素とアンモニアを比較的低温、低圧の
操作条件で、安全かつ効率的に処理し得る方法として、
過酸化水素とアンモニアを含む排水を触媒と接触させて
過酸化水素を分解したのち、アンモニアを揮散させて除
去する方法を提案した。この方法によれば、比較的低
温、低圧で処理することができるが、過酸化水素分解装
置とアンモニア揮散塔の二つの装置が必要である。2. Description of the Related Art Wastewater containing ammonia and hydrogen peroxide is discharged from a semiconductor manufacturing process. Ammonia in wastewater must be removed because it causes eutrophication in closed water bodies such as rivers and lakes. Further, hydrogen peroxide increases the value of COD Mn and thus needs to be decomposed. Conventionally, wastewater containing ammonia and hydrogen peroxide
After performing reduction treatment of hydrogen peroxide with sodium bisulfite or the like or contact treatment with activated carbon, etc.,
Ammonia was removed by biological nitrification denitrification. However, the decomposition of hydrogen peroxide due to the addition of a chemical or the contact with activated carbon is difficult to control, and it is difficult to perform a stable decomposition treatment against fluctuations in the concentration of hydrogen peroxide in wastewater. In addition, removal of ammonia by biological treatment has problems such as generation of sludge, difficulty in maintenance and management, and slow reaction speed, requiring a large device installation area. As a method for solving such a problem and simultaneously decomposing hydrogen peroxide and ammonia in the wastewater, the present applicant has previously disclosed in Japanese Patent Application Laid-Open No. 5-269475 a method in which a wastewater containing hydrogen peroxide and ammonia is used as an 80% wastewater. At ~ 170 ° C,
A method of contacting with a redox catalyst was proposed. According to this method, the treatment can be performed in one step, there is no generation of sludge, and the control of water quality is easy. However, there is a problem that operation at high temperature and high pressure is required and equipment cost is high. The present applicant also discloses in JP-A-2000-51871 that
As a method that can safely and efficiently treat hydrogen peroxide and ammonia in wastewater under relatively low temperature and low pressure operating conditions,
A method was proposed in which wastewater containing hydrogen peroxide and ammonia was brought into contact with a catalyst to decompose hydrogen peroxide, and then ammonia was volatilized and removed. According to this method, the treatment can be performed at a relatively low temperature and a low pressure, but two devices, a hydrogen peroxide decomposing device and an ammonia stripping column, are required.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、排水中に含
まれるアンモニアと過酸化水素を、簡単な単位装置を用
いて、効率よく同時に除去することができるアンモニア
と過酸化水素を含む排水の処理方法を提供することを目
的としてなされたものである。DISCLOSURE OF THE INVENTION The present invention relates to a wastewater containing ammonia and hydrogen peroxide which can efficiently and simultaneously remove ammonia and hydrogen peroxide contained in the wastewater by using a simple unit. The purpose is to provide a processing method.
【０００４】[0004]
【課題を解決するための手段】本発明者らは、上記の課
題を解決すべく鋭意研究を重ねた結果、アンモニアと過
酸化水素を含む排水をアルカリ性条件下に放散塔で処理
することにより、アンモニアを効率的に除去するととも
に、共存する過酸化水素も同時に分解処理し得ることを
見いだし、この知見に基づいて本発明を完成するに至っ
た。すなわち、本発明は、（１）アンモニアと過酸化水
素を含む排水を、アルカリ性条件下に放散塔で処理する
ことを特徴とするアンモニアと過酸化水素を含む排水の
処理方法、及び、（２）アルカリ性条件が、放散塔出口
水のpHが９以上である第１項記載のアンモニアと過酸化
水素を含む排水の処理方法、を提供するものである。Means for Solving the Problems The present inventors have made intensive studies to solve the above-mentioned problems, and as a result, by treating wastewater containing ammonia and hydrogen peroxide in a stripping tower under alkaline conditions, The inventors have found that ammonia can be efficiently removed and coexisting hydrogen peroxide can be simultaneously decomposed, and the present invention has been completed based on this finding. That is, the present invention provides (1) a method for treating wastewater containing ammonia and hydrogen peroxide, wherein the wastewater containing ammonia and hydrogen peroxide is treated in a stripping tower under alkaline conditions, and (2) 2. The method for treating wastewater containing ammonia and hydrogen peroxide according to claim 1, wherein the alkaline condition is such that the pH of the outlet water of the stripping tower is 9 or more.
【０００５】[0005]
【発明の実施の形態】本発明方法においては、アンモニ
アと過酸化水素を含む排水を、アルカリ性条件下に放散
塔で処理する。アルカリ性条件は、放散塔出口水のpHが
９以上であることが好ましい。本発明方法において、排
水中のアンモニアは、物理放散によりキャリアガス中に
移行し、排水中の過酸化水素は、分解したのち生成した
酸素ガスがキャリアガス中へ移行する。本発明方法に用
いる放散塔に特に制限はなく、例えば、充填塔、スプレ
ー塔、サイクロンスクラバー、ベンチュリースクラバ
ー、流動層式吸収塔、ぬれ壁塔などの液分散型装置や、
段塔、気泡塔などのガス分散型装置を用いることができ
る。水中のアンモニア態窒素は、アンモニウムイオンと
アンモニアが次式に示す平衡状態にあり、常温、中性域
では、ほぼ完全にアンモニウムイオンとして存在してい
る。DETAILED DESCRIPTION OF THE INVENTION In the method of the present invention, wastewater containing ammonia and hydrogen peroxide is treated in a stripping tower under alkaline conditions. The alkaline conditions are preferably such that the pH of the outlet water of the stripping tower is 9 or more. In the method of the present invention, the ammonia in the wastewater is transferred into the carrier gas by physical dissipation, and the hydrogen peroxide in the wastewater is decomposed, and the generated oxygen gas is transferred into the carrier gas. There is no particular limitation on the stripping tower used in the method of the present invention, for example, a liquid dispersion type apparatus such as a packed tower, a spray tower, a cyclone scrubber, a venturi scrubber, a fluidized bed absorption tower, a wet wall tower,
A gas dispersion type device such as a column tower or a bubble column can be used. In the ammonium nitrogen in water, ammonium ions and ammonia are in an equilibrium state represented by the following formula, and almost completely exist as ammonium ions in a neutral temperature range at room temperature.
【化１】 このままの状態では、放散塔に空気などのキャリアガス
を吹き込んでも、アンモニア態窒素は放散（ストリッピ
ング）されない。液のpHを高めるか、あるいは、温度を
上げることにより平衡は右へ移行し、溶存アンモニアの
割合が増加する。放散塔で処理する排水をアルカリ性と
することにより、放散によるアンモニアの除去率を高め
ることができる。Embedded image In this state, even if a carrier gas such as air is blown into the stripping tower, the ammonia nitrogen is not stripped. Increasing the pH of the solution or increasing the temperature shifts the equilibrium to the right, increasing the proportion of dissolved ammonia. By making the wastewater treated in the stripping tower alkaline, the removal rate of ammonia by the stripping can be increased.
【０００６】排水中にアンモニアと共存する過酸化水素
も、排水のpHが中性域にある場合は分解が遅いが、排水
をアルカリ条件とすることにより、分解速度を速めるこ
とができる。すなわち、排水をアルカリ条件下に放散塔
で処理することにより、放散によるアンモニアの除去率
と分解による過酸化水素の除去率を共に高めることがで
き、放散塔出口水のpHを９以上とすることにより、アン
モニアと過酸化水素を同時に確実に排水から除去するこ
とができる。排水のpH調整は、pH調整槽を設け、放散塔
出口水のpHを測定して、その値が９以上になるようにpH
調整剤の添加量を制御することができ、あるいは、放散
塔出口水のpHを９以上とするために必要な排水のpH調整
値が経験的に知られている場合は、pH調整槽において所
定のpH値に調整することもできる。排水のpH調整に用い
るpH調整剤に特に制限はなく、例えば、水酸化ナトリウ
ム、水酸化カリウム、水酸化カルシウムなどの水酸化
物、炭酸ナトリウム、炭酸カリウムなどの炭酸塩などを
挙げることができる。本発明方法において、アンモニア
と過酸化水素を含む排水の放散塔における処理は、加熱
下に行うことが好ましく、放散塔出口水の温度が５０〜
１００℃であることが好ましく、放散塔出口水の温度が
８０〜１００℃であることがより好ましい。放散塔出口
水の温度が５０℃未満である条件では、アンモニアと過
酸化水素の除去率が十分に向上しないおそれがある。放
散塔出口水の温度が１００℃を超えるためには、放散塔
を圧力容器とする必要があり、設備費が嵩むおそれがあ
る。排水の加熱方法に特に制限はなく、例えば、放散塔
の処理水との間で熱交換を行って予熱するとともに、放
散塔に蒸気を吹き込んで加熱することができる。[0006] Hydrogen peroxide coexisting with ammonia in wastewater also decomposes slowly when the pH of the wastewater is in a neutral range, but the decomposition rate can be increased by making the wastewater alkaline. That is, by treating the wastewater in a stripping tower under alkaline conditions, both the removal rate of ammonia by stripping and the removal rate of hydrogen peroxide by decomposition can be increased, and the pH of the outlet water of the stripping tower should be 9 or more. Thus, ammonia and hydrogen peroxide can be simultaneously and reliably removed from the wastewater. To adjust the pH of the wastewater, a pH adjustment tank is installed, and the pH of the outlet water of the stripping tower is measured, and the pH is adjusted to 9 or more.
If the amount of the adjusting agent can be controlled, or if the pH adjustment value of the wastewater required for adjusting the pH of the outlet water of the stripping tower to 9 or more is known empirically, the pH adjustment tank is required PH value can be adjusted. There is no particular limitation on the pH adjusting agent used for adjusting the pH of the wastewater, and examples thereof include hydroxides such as sodium hydroxide, potassium hydroxide and calcium hydroxide, and carbonates such as sodium carbonate and potassium carbonate. In the method of the present invention, the treatment of the wastewater containing ammonia and hydrogen peroxide in the stripping tower is preferably performed under heating, and the temperature of the water at the outlet of the stripping tower is 50 to 50.
The temperature is preferably 100 ° C, and more preferably the outlet water temperature of the stripping tower is 80 to 100 ° C. If the temperature of the outlet water of the stripping tower is lower than 50 ° C., the removal rates of ammonia and hydrogen peroxide may not be sufficiently improved. In order for the temperature of the outlet water of the stripping tower to exceed 100 ° C., the stripping tower needs to be a pressure vessel, which may increase equipment costs. There is no particular limitation on the method of heating the wastewater. For example, heat can be exchanged with the treated water in the stripping tower to perform preheating, and the stripping tower can be heated by blowing steam.
【０００７】放散塔より流出する排ガスは、放散された
アンモニアを含むので、アンモニアを酸化分解又は回収
することが好ましい。排ガスを加熱下にアンモニア分解
触媒と接触させることにより、次式に示す反応により、
アンモニアを無害な窒素ガスと水に酸化分解することが
できる。 ４ＮＨ3 ＋ ３Ｏ2 → ２Ｎ2 ＋ ６Ｈ2Ｏ …［２］ アンモニア分解触媒としては、例えば、アルミナ、ゼオ
ライトなどの担体に、ルテニウム、白金などの貴金属を
担持させた触媒を用いることができる。排ガス中に含ま
れるアンモニアの接触分解は、２段階の反応として行う
こともできる。例えば、排ガスを加熱し、白金担持−γ
−アルミナ触媒を充填した酸化触媒塔に通気したのち、
さらにバナジウム−チタニア触媒を充填した還元触媒塔
に通気することにより、アンモニアを低濃度まで分解除
去することができる。過酸化水素の分解により、気相側
の酸素ガス濃度が増加するが、アンモニアの接触分解反
応には影響しない。[0007] Since the exhaust gas flowing out of the stripping tower contains the diffused ammonia, it is preferable to oxidatively decompose or recover the ammonia. By contacting the exhaust gas with the ammonia decomposition catalyst under heating, by the reaction shown in the following formula,
Ammonia can be oxidatively decomposed into harmless nitrogen gas and water. 4NH 3 + 3O 2 → 2N 2 + 6H 2 O [2] As the ammonia decomposition catalyst, for example, a catalyst in which a noble metal such as ruthenium or platinum is supported on a carrier such as alumina or zeolite can be used. The catalytic decomposition of ammonia contained in the exhaust gas can also be performed as a two-stage reaction. For example, the exhaust gas is heated, and
-After venting the oxidation catalyst tower filled with alumina catalyst,
Furthermore, ammonia can be decomposed and removed to a low concentration by ventilating a reduction catalyst tower filled with a vanadium-titania catalyst. The decomposition of hydrogen peroxide increases the concentration of oxygen gas in the gas phase, but does not affect the catalytic decomposition reaction of ammonia.
【０００８】図１は、本発明方法の実施の一態様の工程
系統図である。アンモニアと過酸化水素を含む排水をpH
調整槽１へ送り、アルカリ性条件下に放散塔での処理が
行われるように、pH調整剤を添加する。pH調整は、放散
塔出口水のpHを測定して、その値が９以上になるように
アルカリ調整剤の添加量を制御することができ、あるい
は、放散塔出口水のpHを９以上とするために必要な排水
のpH調整値が経験的に知られている場合は、pH調整槽に
おいて所定のpHに調整することもできる。図１に示す態
様においては、pH調整槽にpH計２を設け、pH調整槽内の
排水のpHが所定の値となるように、pH調整剤を添加す
る。pHが調整された排水を、ポンプ３により送り出し、
熱交換器４において処理水から余熱を回収したのち、放
散塔５の塔頂の液分散器６に供給する。放散塔の下部に
は、キャリアガスとしての空気と加熱用の蒸気を供給
し、流下する排水と向流に接触させる。アンモニアが気
相に移行し、過酸化水素が分解された処理水は、塔底よ
りポンプ７により送り出し、熱交換器４を経由して放流
する。放散塔の塔頂より流出する排ガスは、触媒反応器
８に通気することにより、含有されるアンモニアを酸化
分解し、無害な処理ガスとして放出する。本発明方法に
よれば、アンモニアと過酸化水素を含む排水を、アルカ
リ性条件下に放散塔で処理することにより、アンモニア
を効率的に除去し得るとともに、共存する過酸化水素も
同時に分解処理することができる。また、汚泥などの廃
棄物が発生することもなく、効率的な処理が可能とな
る。FIG. 1 is a flow chart of an embodiment of the method of the present invention. PH of wastewater containing ammonia and hydrogen peroxide
It is sent to the adjusting tank 1 and a pH adjuster is added so that the treatment in the stripping tower is performed under alkaline conditions. The pH can be adjusted by measuring the pH of the water at the outlet of the stripping tower and controlling the addition amount of the alkali adjuster so that the value becomes 9 or more, or setting the pH of the water at the stripping tower outlet to 9 or more. If the pH adjustment value of the wastewater required for this is known empirically, it can be adjusted to a predetermined pH in the pH adjustment tank. In the embodiment shown in FIG. 1, a pH meter 2 is provided in a pH adjusting tank, and a pH adjusting agent is added so that the pH of wastewater in the pH adjusting tank becomes a predetermined value. The pH adjusted wastewater is sent out by the pump 3,
After recovering the residual heat from the treated water in the heat exchanger 4, the residual heat is supplied to the liquid disperser 6 at the top of the stripper 5. Air as a carrier gas and steam for heating are supplied to the lower part of the stripping tower, and are brought into contact with the flowing wastewater and countercurrent. Ammonia shifts to the gas phase, and the treated water in which the hydrogen peroxide is decomposed is sent out from the bottom of the tower by the pump 7 and discharged through the heat exchanger 4. The exhaust gas flowing out from the top of the stripping tower is oxidized and decomposed to ammonia contained therein by passing through the catalytic reactor 8 and released as harmless processing gas. According to the method of the present invention, by treating a wastewater containing ammonia and hydrogen peroxide in a stripper under alkaline conditions, ammonia can be efficiently removed, and simultaneously coexisting hydrogen peroxide is decomposed. Can be. In addition, no waste such as sludge is generated, and efficient treatment can be performed.
【０００９】[0009]
【実施例】以下に、実施例を挙げて本発明をさらに詳細
に説明するが、本発明はこれらの実施例によりなんら限
定されるものではない。 実施例１ アンモニア３,５００mg／Ｌ及び過酸化水素８,０００mg
／Ｌ含有する排水を、図１に示す工程により処理した。
pH調整槽において、排水に水酸化ナトリウム水溶液を添
加してpH１２に調整して、ポンプにより通水速度５０Ｌ
／hrで熱交換器を経由して放散塔へ送り込んだ。放散塔
入口の排水の温度は、７０〜８０℃であった。放散塔
は、内径０.１５ｍ、高さ３.５ｍであり、下方より空気
を流量６ｍ3／hrで送り込むとともに、放散塔出口の処
理水温度が９０〜１００℃になるように蒸気を吹き込ん
だ。処理水は、放散塔出口からポンプで抜き出し、熱交
換器において排水との間で熱交換を行った。放散塔出口
の処理水のpHは、９〜１０であった。処理水中のアンモ
ニア濃度は２０mg／Ｌ以下であり、過酸化水素濃度は３
mg／Ｌ以下であった。放散塔から流出する排ガスは、ア
ンモニア１.７容量％を含んでいた。排ガスを４５０℃
に加熱したのち、断面が一辺０.１５ｍの正方形で高さ
０.５ｍのチタニア系触媒を充填した触媒反応塔に、希
釈空気を含め流量１２ｍ3／hrで送り込んだ。触媒反応
塔から流出する処理ガス中のアンモニア濃度は３０ppm
（容量比）であり、ＮＯx濃度は１０ppm（容量比）以下
であった。 比較例１ 排水のpHを６.９とした以外は、実施例１と同じ条件で
放散塔に通水したところ、処理水中のアンモニア濃度は
１,７００mg／Ｌであり、過酸化水素濃度は４,３００mg
／Ｌであった。実施例１及び比較例１の結果を、第１表
に示す。EXAMPLES The present invention will be described in more detail with reference to the following Examples, which should not be construed as limiting the present invention. Example 1 3,500 mg / L of ammonia and 8,000 mg of hydrogen peroxide
/ L-containing wastewater was treated by the process shown in FIG.
In the pH adjusting tank, an aqueous solution of sodium hydroxide was added to the wastewater to adjust the pH to 12, and the water flow rate was 50 L by a pump.
It was sent to the stripping tower via the heat exchanger at / hr. The temperature of the wastewater at the inlet of the stripping tower was 70 to 80 ° C. The stripping tower has an inner diameter of 0.15 m and a height of 3.5 m, and air is blown in from below at a flow rate of 6 m 3 / hr, and steam is blown so that the temperature of the treated water at the outlet of the stripping tower is 90 to 100 ° C. . The treated water was withdrawn from the outlet of the stripping tower by a pump, and exchanged heat with the wastewater in a heat exchanger. The pH of the treated water at the outlet of the stripping tower was 9 to 10. The ammonia concentration in the treated water is 20 mg / L or less, and the hydrogen peroxide concentration is 3 mg / L.
mg / L or less. The exhaust gas flowing out of the stripping tower contained 1.7% by volume of ammonia. Exhaust gas at 450 ° C
After that, the mixture was fed at a flow rate of 12 m 3 / hr including the dilution air into a catalytic reaction tower filled with a titania-based catalyst having a cross section of 0.15 m and a height of 0.5 m with a side of 0.15 m. The ammonia concentration in the processing gas flowing out of the catalytic reaction tower is 30 ppm
(Volume ratio), and the NOx concentration was 10 ppm (volume ratio) or less. Comparative Example 1 When water was passed through the stripping tower under the same conditions as in Example 1 except that the pH of the wastewater was changed to 6.9, the ammonia concentration in the treated water was 1,700 mg / L, and the hydrogen peroxide concentration was 4%. , 300mg
/ L. Table 1 shows the results of Example 1 and Comparative Example 1.
【００１０】[0010]
【表１】 [Table 1]
【００１１】第１表に見られるように、放散塔出口水の
pHが９以上になるように、pH調整槽において排水のpHを
１２に調整して放散塔に通水した実施例１においては、
アンモニアと過酸化水素が同時にほぼ完全に除去された
処理水が得られている。これに対して、排水のpHを６.
９として放散塔に通水した比較例１では、アンモニア、
過酸化水素ともにほぼ半減するにとどまっている。As can be seen in Table 1, the outlet water of the stripping tower
In Example 1 in which the pH of the wastewater was adjusted to 12 in the pH adjusting tank so that the pH became 9 or more and the water was passed through the stripping tower,
Processed water from which ammonia and hydrogen peroxide have been almost completely removed at the same time is obtained. On the other hand, the pH of the wastewater was 6.
In Comparative Example 1 in which water was passed through the stripping tower as No. 9, ammonia,
Hydrogen peroxide is almost halved.
【００１２】[0012]
【発明の効果】本発明方法によれば、簡単な単位装置を
用いてアンモニアと過酸化水素を含む排水を処理して、
アンモニアと過酸化水素を同時に除去することができ、
しかも廃棄物が発生しない。According to the method of the present invention, waste water containing ammonia and hydrogen peroxide is treated using a simple unit device,
Ammonia and hydrogen peroxide can be removed simultaneously,
Moreover, no waste is generated.
【図１】図１は、本発明方法の実施の一態様の工程系統
図である。FIG. 1 is a process flow chart of an embodiment of the method of the present invention.
１ pH調整槽 ２ pH計 ３ ポンプ ４ 熱交換器 ５ 放散塔 ６ 液分散器 ７ ポンプ ８ 触媒反応器 1 pH adjustment tank 2 pH meter 3 Pump 4 Heat exchanger 5 Dispersion tower 6 Liquid disperser 7 Pump 8 Catalytic reactor
───────────────────────────────────────────────────── フロントページの続き (72)発明者 上笹貫 透 東京都新宿区西新宿三丁目４番７号 栗田 工業株式会社内 Ｆターム(参考） 4D037 AA13 AB11 AB12 BA23 BB05 CA14 ────────────────────────────────────────────────── ─── Continuing on the front page (72) Inventor Toru Uesasa Kan 3-4-7 Nishishinjuku, Shinjuku-ku, Tokyo F-term in Kurita Industrial Co., Ltd. 4D037 AA13 AB11 AB12 BA23 BB05 CA14
Claims (2)
ルカリ性条件下に放散塔で処理することを特徴とするア
ンモニアと過酸化水素を含む排水の処理方法。1. A method for treating wastewater containing ammonia and hydrogen peroxide, wherein the wastewater containing ammonia and hydrogen peroxide is treated in a stripping tower under alkaline conditions.
以上である請求項１記載のアンモニアと過酸化水素を含
む排水の処理方法。2. The alkaline condition is such that the pH at the outlet of the stripping tower is 9
The method for treating wastewater containing ammonia and hydrogen peroxide according to claim 1.
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103964522A (en) * | 2013-01-30 | 2014-08-06 | 栗田工业株式会社 | Treatment method and device for water containing hydrogen peroxide and ammonia |
| WO2022092086A1 (en) * | 2020-10-30 | 2022-05-05 | 栗田工業株式会社 | Exhaust gas treatment facility |
| JP2022122616A (en) * | 2021-02-10 | 2022-08-23 | 栗田工業株式会社 | Exhaust disposal facility |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR101793968B1 (en) * | 2015-04-15 | 2017-11-07 | 주식회사 네패스 | Apparatus for decomposition reaction of hydrogen peroxide |
Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS516352A (en) * | 1974-07-09 | 1976-01-19 | Mitsubishi Heavy Ind Ltd | ANMONIAGANJUHAIEKINO SHORIHOHO |
| JPH0347592A (en) * | 1989-07-17 | 1991-02-28 | Ebara Infilco Co Ltd | Removal of hydrogen peroxide |
-
2000
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Patent Citations (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS516352A (en) * | 1974-07-09 | 1976-01-19 | Mitsubishi Heavy Ind Ltd | ANMONIAGANJUHAIEKINO SHORIHOHO |
| JPH0347592A (en) * | 1989-07-17 | 1991-02-28 | Ebara Infilco Co Ltd | Removal of hydrogen peroxide |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN103964522A (en) * | 2013-01-30 | 2014-08-06 | 栗田工业株式会社 | Treatment method and device for water containing hydrogen peroxide and ammonia |
| KR20140097983A (en) | 2013-01-30 | 2014-08-07 | 쿠리타 고교 가부시키가이샤 | Method and apparatus for treating water containing hydrogen peroxide and ammonia |
| JP2014144445A (en) * | 2013-01-30 | 2014-08-14 | Kurita Water Ind Ltd | Method and apparatus for treating water containing hydrogen peroxide and ammonia |
| CN103964522B (en) * | 2013-01-30 | 2017-10-13 | 栗田工业株式会社 | The processing method and processing device of water containing hydrogen peroxide and ammonia |
| WO2022092086A1 (en) * | 2020-10-30 | 2022-05-05 | 栗田工業株式会社 | Exhaust gas treatment facility |
| JP2022122616A (en) * | 2021-02-10 | 2022-08-23 | 栗田工業株式会社 | Exhaust disposal facility |
| JP7230940B2 (en) | 2021-02-10 | 2023-03-01 | 栗田工業株式会社 | Exhaust gas treatment equipment |
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