JPS6125694A - Oxidation treatment of organic waste water - Google Patents
Oxidation treatment of organic waste waterInfo
- Publication number
- JPS6125694A JPS6125694A JP14435884A JP14435884A JPS6125694A JP S6125694 A JPS6125694 A JP S6125694A JP 14435884 A JP14435884 A JP 14435884A JP 14435884 A JP14435884 A JP 14435884A JP S6125694 A JPS6125694 A JP S6125694A
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- Prior art keywords
- activated carbon
- oxidizing agent
- reaction
- oxidation
- treated
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- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は，有機性廃水を過酸化水素又は次亜塩素酸ナト
リウム等の酸化剤で酸化処理する方法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for oxidizing organic wastewater with an oxidizing agent such as hydrogen peroxide or sodium hypochlorite.
従来，有機性廃水の酸化処理方法としては，過酸化水素
又は次亜塩素酸ナトリウム等の酸化剤を被処理液に注入
し，反応槽内で被処理液中の有機物を酸化分解させ，余
剰の酸化剤を後段で亜坑酸ナトリウム又は重亜硫酸ナト
リウム等の還元剤で中和する方法，酸化性ガス，例えば
オノ°ン等を被処理液に接触させて酸化処理する方法，
紫外線照射又は電気化学的な酸化処理方法が知られてい
る。Conventionally, the oxidation treatment method for organic wastewater involves injecting an oxidizing agent such as hydrogen peroxide or sodium hypochlorite into the liquid to be treated, oxidizing and decomposing the organic matter in the liquid in a reaction tank, and removing the excess. A method in which the oxidizing agent is neutralized with a reducing agent such as sodium aphrite or sodium bisulfite at a later stage; a method in which an oxidizing gas such as onone is brought into contact with the liquid to be treated;
Ultraviolet irradiation or electrochemical oxidation treatment methods are known.
これらの処理方法のうち，オノ゛ンや紫外線等による酸
化処理方法は装置が複雑となるばかりでなく，運転コス
トも酸化剤を用いる方法に比べて。Among these treatment methods, oxidation treatment methods using onion or ultraviolet rays not only require more complicated equipment, but also have higher operating costs than methods that use oxidizers.
高価となる等の欠点を有するため，通常の酸化処理は酸
化剤を用いた薬品酸化が行われている。しかしながら、
この薬品酸化処理は被処理液中の有機物の酸化速度が運
いため、長時間接触させなければ充分な処理効果が得ら
れないと同時に、残存する酸化剤を中和する際に別途、
還元剤を必要とする欠点がある。Since it has drawbacks such as being expensive, chemical oxidation using an oxidizing agent is commonly used as the oxidation treatment. however,
In this chemical oxidation treatment, the rate of oxidation of organic matter in the liquid to be treated is affected, so sufficient treatment effects cannot be obtained unless contact is made for a long time.
It has the disadvantage of requiring a reducing agent.
また、この場合に、酸化速度を上げるために金属触媒１
例えば酸化ニッケル、酸化マンガン等を用いる方法も検
討されているが、必ずしも満足する結果は得られていな
い。In this case, in order to increase the oxidation rate, a metal catalyst 1
For example, methods using nickel oxide, manganese oxide, etc. have been considered, but satisfactory results have not always been obtained.
本発明の目的は、前記の従来技術の欠点を解消し、被処
理液中の有機物に対する酸化速度を高め。An object of the present invention is to eliminate the drawbacks of the prior art described above and increase the rate of oxidation of organic substances in the liquid to be treated.
従来の酸化処理に比べて優れた処理効果が得られ。Superior treatment effects can be obtained compared to conventional oxidation treatment.
残存する酸化剤の処理を還元剤を用いることなく行うこ
とのできる有機性廃水の処理方法を提供することにある
。An object of the present invention is to provide a method for treating organic wastewater in which residual oxidizing agents can be treated without using reducing agents.
〔発明の要点」
この目的は９本発明によれば、有機物の酸化工程及び残
存酸化剤の分解工程をそれぞれ活性炭を媒体として行う
ことにより達成できる。即ち１本発明による有機性廃水
の処理方法は廃水を酸化剤と混合して活性炭を浮遊させ
た反応槽内に流入させ、酸化剤として過酸化水素を用い
る場合は反応ｐＨ３〜５９次亜塩素酸ナトリウムを用い
る場合は反応ｐＨ９〜１０とし、有機物を酸化する工程
と、その耐化工程からの流出液を別の活性炭を浮遊させ
た反応槽に流入させて残存する酸化剤を分解させる工程
から成ることを特徴とする。[Summary of the Invention] According to the present invention, this object can be achieved by carrying out the step of oxidizing organic matter and the step of decomposing the residual oxidant, respectively, using activated carbon as a medium. Namely, in the method for treating organic wastewater according to the present invention, wastewater is mixed with an oxidizing agent and flows into a reaction tank in which activated carbon is suspended, and when hydrogen peroxide is used as the oxidizing agent, the reaction pH is 3 to 59 hypochlorous acid. When using sodium, the reaction pH is adjusted to 9 to 10, and the process consists of a step of oxidizing organic matter, and a step of flowing the effluent from the resistant process into another reaction tank in which activated carbon is suspended to decompose the remaining oxidizing agent. It is characterized by
本発明は、酸化剤による有機物の酸化分解作用が多孔性
固体表面で活発に行われ、かつ有機物濃度が高いほど酸
化速度が上昇するという２つの物理的特性を応用する手
段として、酸化処理に活性炭を媒体として用いるもので
ある。即ち１本発明は、被処理液中の有機物を多孔性活
性炭の表面に吸着させ、高濃度の有機物を活性炭表面に
保持する吸着濃縮作用と高濃度の有機物が保持された活
性炭表面で酸化剤を作用させ、効率よく酸化処理する酸
化分解作用更に、有機物の酸化分解後に残留麺する酸化
剤を別の活性炭と接触させて酸化剤の自己分解速度を上
昇させ、無毒化する作用を反応槽内で連続的に行う様、
構成したものである。The present invention utilizes activated carbon for oxidation treatment as a means of applying two physical properties: the oxidative decomposition action of organic matter by an oxidizing agent is actively carried out on the surface of a porous solid, and the oxidation rate increases as the concentration of organic matter increases. is used as a medium. That is, 1. The present invention adsorbs organic substances in the liquid to be treated on the surface of porous activated carbon, and has an adsorption concentration effect that retains high-concentration organic substances on the activated carbon surface, and an oxidizing agent on the activated carbon surface that retains high-concentration organic substances. In addition, the oxidizing agent that remains after the oxidative decomposition of organic matter is brought into contact with another activated carbon to increase the self-decomposition rate of the oxidizing agent and detoxify it in the reaction tank. Do it continuously,
It is composed of
次に図面に基づいて９本発明を詳述する。第１図は本発
明の酸化処理方法を実施する装置の一実施例を示すフロ
ーシートである。被処理液は、まずｐＨ調整槽ｌで所定
の反応ｐＨ（過酸化水素の場合：反応ｐＨ３〜５９次亜
塩素酸ソーダの場合：反応ｐＨ９〜１０）に調整され、
第一反応槽２に流入する。第１反応槽２には活性炭が浮
遊しており、ｆｆ化化性注入ポンプ６槽内に過酸化水素
又は次亜機素酸ナトリウム等の酸化剤が注入される。Next, the present invention will be explained in detail based on the drawings. FIG. 1 is a flow sheet showing an embodiment of an apparatus for carrying out the oxidation treatment method of the present invention. The liquid to be treated is first adjusted to a predetermined reaction pH (for hydrogen peroxide: reaction pH 3 to 59, for sodium hypochlorite: reaction pH 9 to 10) in a pH adjustment tank 1,
It flows into the first reaction tank 2. Activated carbon is floating in the first reaction tank 2, and an oxidizing agent such as hydrogen peroxide or sodium hypoxite is injected into the ff-forming injection pump 6 tank.
被処理液中の有機物は、まず活性炭の有機物吸着作用に
より活性炭表面の細孔内部に吸着され、徐々に有機物濃
度が高められるが（吸着−濃縮作用）この作用と同時に
槽内に注入された酸化剤が多孔性の活性炭表面で分解し
、有機物を分解する反応基（過酸化水素の場合は０５ジ
カル）が遊離し。The organic matter in the liquid to be treated is first adsorbed inside the pores on the surface of the activated carbon by the organic matter adsorption effect of the activated carbon, and the concentration of organic matter gradually increases (adsorption-concentration effect). The agent decomposes on the surface of porous activated carbon, and a reactive group (05 radical in the case of hydrogen peroxide) that decomposes organic matter is liberated.
活性炭表面に吸着された有機物を酸化分解する。Oxidatively decomposes organic substances adsorbed on the surface of activated carbon.
（酸化分解作用）
前記の吸着−濃縮作用と酸化分解作用とは同一活性炭表
面で行われ、単一活性炭表面での両反応は見掛は上、平
衡状態に近くなっている。従って。(Oxidative decomposition action) The adsorption-concentration action and the oxidative decomposition action described above are performed on the same activated carbon surface, and both reactions on the single activated carbon surface appear to be close to an equilibrium state. Therefore.
活性炭吸着で一般的に見られる破過（有機物吸肩の飽和
点）は生じにくい。こうして吸着−濃縮作用及び酸化分
解作用を受けた被処理液は第１反応槽内で活性炭と分離
され、ｐＨ調整槽３に流入する。Breakthrough (saturation point of the organic absorption shoulder), which is commonly seen in activated carbon adsorption, is unlikely to occur. The liquid to be treated thus subjected to the adsorption-concentration action and the oxidative decomposition action is separated from the activated carbon in the first reaction tank and flows into the pH adjustment tank 3.
被処理液はｐＨ調整槽３で酸化剤の分解７）Ｈ（過酸化
水素の場合：反応ｐＨ９〜１２１次亜塩素酸ソーダの場
合：反応ｐＨ３〜５）に調整され、第２反応槽４に流入
する。第２反応槽４は第１反応槽と同様に活性炭が浮遊
しておシ、ここで残存する酸化剤、即ち有機物の酸化分
解が終了した後に残留する酸化剤は、更に活性炭表面で
自己分解を促進され、迅速に分解する。従って、処理水
中には酸化剤が残留することなく、従来の酸化処理法に
使用された亜硫酸ナトリウム等の還元剤は不要となる。The liquid to be treated is adjusted to decomposition of the oxidizing agent 7)H (for hydrogen peroxide: reaction pH 9-121, for sodium hypochlorite: reaction pH 3-5) in the pH adjustment tank 3, and then transferred to the second reaction tank 4. Inflow. In the second reaction tank 4, activated carbon is suspended in the same way as in the first reaction tank, and the remaining oxidizing agent, that is, the oxidizing agent remaining after the oxidative decomposition of organic matter is completed, undergoes further self-decomposition on the surface of the activated carbon. Accelerated and rapid decomposition. Therefore, no oxidizing agent remains in the treated water, and reducing agents such as sodium sulfite used in conventional oxidation treatment methods become unnecessary.
残存酸化剤の分解が終了し、無害化された被処理液は第
２反応槽内で活性炭と分離されｐＨ調整槽５で中和され
た後、放流又は再利用される。After the decomposition of the remaining oxidizing agent is completed, the detoxified liquid to be treated is separated from the activated carbon in the second reaction tank, neutralized in the pH adjustment tank 5, and then discharged or reused.
こうして９本発明によれば、有機性廃水を迅速に効率よ
く酸化処理することができ、しかも、残存酸化剤を除去
するための還元剤を必要とせず優れた処理効果が達成さ
れる。Thus, according to the present invention, organic wastewater can be oxidized quickly and efficiently, and excellent treatment effects can be achieved without the need for a reducing agent to remove residual oxidizing agents.
次に実施例に基づいて本発明を詳述するが１本発明はこ
れに限定されるものではない。Next, the present invention will be described in detail based on Examples, but the present invention is not limited thereto.
〔実施例１〕
機械工場廃水の２次処理水（ＣＯＤ含有量１１０ｗ１／
ｌ）を用いて、第１図に示したフローシートの酸化工程
及び分解工程、それぞれの基本実験を行った。また７本
実験に使用した活性炭はあらかじめ有機物吸着の破過点
に達しているスはントカーボンである。[Example 1] Secondary treated machine factory wastewater (COD content 110w1/
Basic experiments for the oxidation process and the decomposition process of the flow sheet shown in FIG. 1 were conducted using 1). In addition, the activated carbon used in the seven experiments is a short carbon that has already reached the breakthrough point of organic matter adsorption.
第２図は第１反応槽（酸化工程）で酸化剤として過酸化
水素を用いた場合の接触時間とＣＯＤ除去量との関係を
示し、第３図は反応ｐＨとＣＯＤ除去ｌとの関係を示す
。第２図及び以下の記載において残存ＣＯＤは残存酸化
剤を補正した数値で示している。第２図及び第３図から
れかるように従来法（活性炭ｏｍｔ７ｔ＞では接触時間
が５時間経過しても、ＣＯＤが３０■／ｌであるのに対
し。Figure 2 shows the relationship between the contact time and the amount of COD removed when hydrogen peroxide is used as the oxidant in the first reaction tank (oxidation step), and Figure 3 shows the relationship between the reaction pH and the amount of COD removed. show. In FIG. 2 and the following description, the residual COD is shown as a value corrected for the residual oxidant. As can be seen from FIGS. 2 and 3, in contrast to the conventional method (activated carbon omt7t), the COD was 30 μ/l even after 5 hours of contact time.
本発明方法である活性炭存在下による酸化では活性炭量
を増加させるにつれて、ＣＯＤの除去効果が上昇し、活
性炭２０，０００η／ｌの場合では接触時間２時間で既
にＣＯＤは１０■／ｌとなっている。また、この時の反
応ｐＨは３〜５が最も好ましいことが分かる。In the method of the present invention, oxidation in the presence of activated carbon, the COD removal effect increases as the amount of activated carbon increases, and in the case of activated carbon of 20,000 η/l, the COD was already 10 η/l after 2 hours of contact time. There is. It is also understood that the reaction pH at this time is most preferably 3 to 5.
第４図は第１反応槽に使用する酸化剤を次亜塩素酸ナト
リウムとした場合の接触時間とＣＯＤ除去量との関係を
示し、第５図は反応ｐＨとＣＯＤ除去量との関係を示す
。Figure 4 shows the relationship between the contact time and the amount of COD removed when the oxidizing agent used in the first reaction tank is sodium hypochlorite, and Figure 5 shows the relationship between the reaction pH and the amount of COD removed. .
第４図及び第５図かられかるように、酸化剤として次亜
塩素酸ナトリウムを用いた場合も１本発明方法は従来法
に比べ、ＣＯＤ除去効果が大きい。As can be seen from FIGS. 4 and 5, even when sodium hypochlorite is used as the oxidizing agent, the method of the present invention has a greater COD removal effect than the conventional method.
また、この時の反応ｐＨは、過酸化水素−を用いた場合
と異なり、ｐＨ９〜１０のアルカリ状態が最も好ましい
ことがわかる。Further, it can be seen that the reaction pH at this time is most preferably an alkaline state of pH 9 to 10, unlike the case where hydrogen peroxide is used.
即ち１本発明方法は酸化剤として過酸化水素及び次亜塩
素酸ナトリウムのいずれを使用しても。Namely, the method of the present invention can be used regardless of whether hydrogen peroxide or sodium hypochlorite is used as the oxidizing agent.
従来法と比べて酸化速度及び処理効果の両面において著
しく優れている。This method is significantly superior to conventional methods in terms of both oxidation speed and treatment effect.
第６図は、第２反応槽（残留酸化剤の分解工程）Ｋおけ
る残留酸化剤の分解ｐＨと残留濃度との関係を示す。第
６図かられかるように、酸化剤として過酸化水素を用い
た場合と１次亜塩素酸ナトリウムを用いた場合とでは９
分解ｐＨの好適範囲が異なり、残留過酸化水素の好適分
解ｐＨは９〜１２、残留次亜塩素酸ナトリウムの好適分
解ｐＨは３〜５であり、このｐＨ条件において、接触時
間を２時間とすることで残留醪化剤の自己分解が終了す
ることがわかる。FIG. 6 shows the relationship between the decomposition pH of the residual oxidant in the second reaction tank (residual oxidant decomposition step) K and the residual concentration. As shown in Figure 6, when hydrogen peroxide is used as the oxidizing agent and when primary sodium hypochlorite is used, the difference is 9.
The preferred decomposition pH ranges are different; the preferred decomposition pH for residual hydrogen peroxide is 9 to 12, and the preferred decomposition pH for residual sodium hypochlorite is 3 to 5. Under these pH conditions, the contact time is 2 hours. It can be seen that this completes the self-decomposition of the residual thickening agent.
〔実施例２〕 実施例１と同じ機械工場の２次処理水を用いて。[Example 2] Using the same secondary treated water from the machine shop as in Example 1.
第１図に示すフローシートで連続処理を行った。Continuous processing was carried out using the flow sheet shown in FIG.
酸化剤として過酸化水素をＣＯＤに対して、１．５倍用
いて第１反応槽の接触時間を４時間１及応ｐＨ３，活性
炭浮遊量１０，０００〜／１．第２反応槽の接触時間を
２時間９及応ｐＨ１０，活性炭浮遊１５ｏＯｏ■／ｌで
処理し１通水倍率（原水量／活性炭容量）ｋ５０００倍
まで実施した。処理水質及び処理ＣＯＤ量を測定し、結
果を第７図に示す。Hydrogen peroxide was used as an oxidizing agent at a rate of 1.5 times the COD, and the contact time in the first reaction tank was set to 4 hours at a pH of 3, and the amount of suspended activated carbon was 10,000 to 1. The contact time in the second reaction tank was 2 hours at 9, pH 10 and activated carbon suspended at 150Oo/l until the water flow rate (raw water amount/activated carbon volume) was 5000 times. The treated water quality and treated COD amount were measured, and the results are shown in Figure 7.
運転期間を通じて、第１反応検出口の残存ＣＯＤはｌＯ
■／を前後（残存酸化剤のＣＯＤを補正）で安定してお
り、この時の残存酸化剤は２０〜５０■／ｌであった。Throughout the operation period, the residual COD at the first reaction detection port is lO
It was stable around (COD of residual oxidant was corrected) around (1)/l, and the residual oxidant at this time was 20 to 50 (2)/l.
残存酸化剤は第２反応槽で分解され放流水（第２反応検
出口）には殆ど検出されなかった。The remaining oxidant was decomposed in the second reaction tank and was hardly detected in the discharged water (second reaction detection port).
また、処理ＣＯＤ量の累積値をみると１通水倍量５００
０倍において１．１９−Ｃｏｔ）／Ｓ’−活性炭となり
。In addition, looking at the cumulative value of the amount of COD treated, the amount of water per passage is 500.
At 0x, it becomes 1.19-Cot)/S'-activated carbon.
通常の活性炭の破過点帆４５’−ＣＯＤ／ｒ−活性炭と
比べて約３倍の結果を得た。これは１本発明方法では活
性炭表面で有機物の吸着−濃縮と酸化分解との両反応が
平衡して進行しているため、破過現象が生じにくいもの
と考えられる。なお１本発明方法は活性炭の浮遊量及び
酸化剤注入ｔを変化させることで、実装置における水量
、水質変動にも容易に灼応できる特徴がある。The breakthrough point of normal activated carbon was about 3 times as high as that of 45'-COD/r-activated carbon. This is thought to be because, in the method of the present invention, both reactions of adsorption and concentration of organic matter and oxidative decomposition proceed in equilibrium on the surface of the activated carbon, so that the breakthrough phenomenon is unlikely to occur. Note that the method of the present invention has a feature that it can easily respond to changes in water amount and water quality in an actual device by changing the suspended amount of activated carbon and the oxidizing agent injection t.
第１図は本発明方法を実施する装置の一実施例を示すフ
ローシート、第２図は過酸化水素を用いた有機物の酸化
工程におけるＣＯＤの時間変化図。
第３図は同じく酸化工程における反応ｐＨとの関係図、
第４図は次亜塩素酸ナトリウムを用いた有機物の酸化工
礎におけるＣＯＤの時間変化図、第５図は同じく酸化工
程における反応ｐＨとの関係図、第６図は残留酸化剤の
分解工程における分解７）Ｈとの関係図、第７図は過酸
化水素を用いた酸化工程と分解工程の連続結果で、ｂる
。
１＝−ｐＨ調整槽 ２・・・第１反応槽３ ・ｐ
Ｈ調整槽 ４・・・第２反応槽５・・ｐＨ調整槽
６・・酸化剤注入ポンシフ ・被処理液移送ポ
ンプ ８ ・・酸・アルカリ注入ポンプ。FIG. 1 is a flow sheet showing an example of an apparatus for carrying out the method of the present invention, and FIG. 2 is a time change diagram of COD in an oxidation process of organic matter using hydrogen peroxide. Figure 3 is also a relationship diagram with reaction pH in the oxidation process,
Figure 4 is a time change diagram of COD in the oxidation foundation of organic matter using sodium hypochlorite, Figure 5 is a diagram of the relationship with reaction pH in the oxidation process, and Figure 6 is a diagram of the relationship between the COD and the reaction pH in the decomposition process of residual oxidant. Decomposition 7) Relationship diagram with H, Figure 7 shows the successive results of the oxidation step using hydrogen peroxide and the decomposition step. 1=-pH adjustment tank 2...1st reaction tank 3 ・p
H adjustment tank 4...Second reaction tank 5...pH adjustment tank 6...Oxidizer injection pump - To be treated liquid transfer pump 8...Acid/alkali injection pump.
Claims (2)
ム等の酸化剤を作用させ、廃水中の有機物を酸化処理す
る方法において、廃水を酸化剤と混合して活性炭を浮遊
させた反応槽内に流入させ有機物を酸化させる酸化工程
と、その酸化工程からの流出液を別の活性炭を浮遊させ
た反応槽に流入させ残留する酸化剤を分解する工程から
成ることを特徴とする有機性廃水の酸化処理方法。(1) In a method of oxidizing organic matter in wastewater by applying an oxidizing agent such as hydrogen peroxide or sodium hypochlorite to organic wastewater, a reaction tank is used in which wastewater is mixed with an oxidizing agent and activated carbon is suspended. Organic wastewater is characterized by comprising an oxidation step in which the organic matter is oxidized by the oxidizing agent, and a step in which the effluent from the oxidation step is flowed into another reaction tank in which activated carbon is suspended to decompose the remaining oxidizing agent. oxidation treatment method.
化工程での反応ｐＨを３〜５、分解工程での反応ｐＨを
９〜１２とし、酸化剤として、次亜塩素酸ナトリウムを
作用させる場合は酸化工程での反応ｐＨを９〜１０、分
解工程での反応ｐＨを３〜５とすることを特徴とする特
許請求の範囲第一項記載の酸化処理方法。(2) When using hydrogen peroxide as an oxidizing agent, the reaction pH in the oxidation step is 3 to 5, and the reaction pH in the decomposition step is 9 to 12, and sodium hypochlorite is used as the oxidizing agent. The oxidation treatment method according to claim 1, wherein the reaction pH in the oxidation step is 9 to 10, and the reaction pH in the decomposition step is 3 to 5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14435884A JPS6125694A (en) | 1984-07-13 | 1984-07-13 | Oxidation treatment of organic waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP14435884A JPS6125694A (en) | 1984-07-13 | 1984-07-13 | Oxidation treatment of organic waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6125694A true JPS6125694A (en) | 1986-02-04 |
Family
ID=15360244
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP14435884A Pending JPS6125694A (en) | 1984-07-13 | 1984-07-13 | Oxidation treatment of organic waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6125694A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62241596A (en) * | 1986-04-11 | 1987-10-22 | Kurita Water Ind Ltd | Treatment of waste water containing organic matter |
| JPH04300695A (en) * | 1991-03-28 | 1992-10-23 | Ebara Infilco Co Ltd | Method and apparatus for treating organic waste water |
| KR20010088752A (en) * | 2001-08-30 | 2001-09-28 | 염복철 | The treatment method of industrial wastewaters having a hard decomposition activity |
| KR100434392B1 (en) * | 2001-08-30 | 2004-06-04 | 삼구화학공업 주식회사 | The treatment method of industrial wastewaters utilizing perchloric acid salt |
| US7985877B2 (en) | 2006-06-05 | 2011-07-26 | Daikin Industries, Ltd. | Carboxylic acid compound, use thereof, and process for producing the same |
| US8013182B2 (en) | 2007-11-13 | 2011-09-06 | Daikin Industries, Ltd. | Carboxylic acid ester, use of the same, and method for producing the same |
| US8022245B2 (en) | 2006-07-06 | 2011-09-20 | Daikin Industries, Ltd. | Alpha-fluoromethoxycarboxylic ester, process for producing the alpha-fluoromethoxycarboxylic ester, and process for producing sevoflurane |
-
1984
- 1984-07-13 JP JP14435884A patent/JPS6125694A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS62241596A (en) * | 1986-04-11 | 1987-10-22 | Kurita Water Ind Ltd | Treatment of waste water containing organic matter |
| JPH04300695A (en) * | 1991-03-28 | 1992-10-23 | Ebara Infilco Co Ltd | Method and apparatus for treating organic waste water |
| KR20010088752A (en) * | 2001-08-30 | 2001-09-28 | 염복철 | The treatment method of industrial wastewaters having a hard decomposition activity |
| KR100434392B1 (en) * | 2001-08-30 | 2004-06-04 | 삼구화학공업 주식회사 | The treatment method of industrial wastewaters utilizing perchloric acid salt |
| US7985877B2 (en) | 2006-06-05 | 2011-07-26 | Daikin Industries, Ltd. | Carboxylic acid compound, use thereof, and process for producing the same |
| US8022245B2 (en) | 2006-07-06 | 2011-09-20 | Daikin Industries, Ltd. | Alpha-fluoromethoxycarboxylic ester, process for producing the alpha-fluoromethoxycarboxylic ester, and process for producing sevoflurane |
| US8013182B2 (en) | 2007-11-13 | 2011-09-06 | Daikin Industries, Ltd. | Carboxylic acid ester, use of the same, and method for producing the same |
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