JP2000301174A - Wastewater treatment equipment - Google Patents
Wastewater treatment equipmentInfo
- Publication number
- JP2000301174A JP2000301174A JP11111111A JP11111199A JP2000301174A JP 2000301174 A JP2000301174 A JP 2000301174A JP 11111111 A JP11111111 A JP 11111111A JP 11111199 A JP11111199 A JP 11111199A JP 2000301174 A JP2000301174 A JP 2000301174A
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- JP
- Japan
- Prior art keywords
- raw water
- ozone
- membrane separation
- membrane
- separation device
- 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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- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
(57)【要約】
【課題】 膜汚染の防止のために原水をオゾン酸化処理
した後、膜分離処理する用排水処理装置において、オゾ
ン反応塔を設けることなく、オゾンの吸収効率及びオゾ
ンによる原水中のＴＯＣ成分の酸化分解効率を高め、長
期に亘り膜分離装置を安定かつ効率的に運転する。
【解決手段】 原水槽１と、膜分離装置２と、オゾン注
入手段３（３Ａ，３Ｂ）とを備えた用排水処理装置。オ
ゾン注入手段３Ａ，３Ｂは、原水槽１から膜分離装置２
へ原水を送給するための原水送給配管１２と、膜分離装
置２の濃縮水を原水槽１に戻すための濃縮水戻り配管１
３とに連絡している。
PROBLEM TO BE SOLVED: To provide an ozone oxidation treatment for raw water in order to prevent membrane contamination, and then, in a wastewater treatment apparatus for membrane separation treatment, to provide an ozone absorption efficiency and ozone generation efficiency without providing an ozone reaction tower. Increase the efficiency of oxidative decomposition of TOC components in water, and operate the membrane separation device stably and efficiently for a long period of time. SOLUTION: A waste water treatment apparatus provided with a raw water tank 1, a membrane separation device 2, and an ozone injection means 3 (3A, 3B). The ozone injecting means 3A, 3B is provided between the raw water tank 1 and the membrane separation device 2
Raw water supply pipe 12 for supplying raw water to concentrated water return pipe 1 for returning concentrated water of membrane separation device 2 to raw water tank 1
3 has been contacted.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、原水をオゾン酸化
処理し、オゾン処理水を膜分離処理する用排水処理装置
に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a wastewater treatment apparatus for subjecting raw water to ozone oxidation and membrane separation of ozonated water.
【０００２】[0002]
【従来の技術及び先行技術】従来、用水ないし排水処理
における逆浸透（ＲＯ）膜分離装置等の浄化設備の前処
理システムとしては、一般的に、凝集・沈殿・砂濾過か
らなるシステムが採用されていたが、この前処理システ
ムでは、原水の有機物濃度が高まると、塩化第二鉄、ポ
リ塩化アルミニウム、硫酸アルミニウム等の凝集剤を多
量に添加する必要があるという欠点がある。また、原水
の水質変動に対応した凝集剤添加量の調整が必要であ
り、適正な添加量制御が行われない場合には、処理水の
水質が悪化するという問題もあった。2. Description of the Related Art Conventionally, as a pretreatment system of a purification facility such as a reverse osmosis (RO) membrane separation device in water or wastewater treatment, a system comprising coagulation, sedimentation and sand filtration is generally employed. However, this pretreatment system has a drawback that when the organic matter concentration of the raw water increases, a large amount of a coagulant such as ferric chloride, polyaluminum chloride, or aluminum sulfate must be added. In addition, it is necessary to adjust the addition amount of the flocculant in accordance with the water quality fluctuation of the raw water, and if the addition amount control is not performed properly, there is a problem that the quality of the treated water deteriorates.
【０００３】このため、このような旧来の前処理プロセ
スに替わって、精密濾過（ＭＦ）膜や限外濾過（ＵＦ）
膜等を用いた膜分離処理が採用されるようになってきて
いる。ＭＦ膜やＵＦ膜によれば、凝集剤を添加すること
なく、又は微量の凝集剤の添加だけで、後段のＲＯ膜を
汚染させるコロイド状成分を除去することができ、ＲＯ
膜の汚染を抑止してその薬品洗浄間隔を延ばし、ＲＯ膜
分離装置の運転を効率化させることができる。[0003] For this reason, microfiltration (MF) membranes and ultrafiltration (UF) have been replaced by such conventional pretreatment processes.
Membrane separation processing using a membrane or the like has been adopted. According to the MF membrane and the UF membrane, a colloidal component that contaminates a subsequent RO membrane can be removed without adding a coagulant or only by adding a small amount of a coagulant.
It is possible to suppress the contamination of the membrane, extend the chemical cleaning interval, and increase the efficiency of the operation of the RO membrane separation apparatus.
【０００４】しかし、近年、工業用水や下水道の取水水
源等の有機物汚染により、用水処理における原水中には
微生物代謝産物である高分子状のフミン酸やフルボ酸か
らなるＴＯＣ成分が増加している。このため、このよう
な膜分離処理による前処理を行うシステムでは、前処理
用のＭＦ膜やＵＦ膜の膜面に、原水中のＴＯＣ成分であ
る高分子状のフミン酸やフルボ酸が吸着ないし沈着して
膜を汚染させ、膜の濾過抵抗を高める傾向が増々強くな
ってきている。このような高分子状のフミン酸やフルボ
酸による膜汚染が生じた場合には、ＭＦ膜やＵＦ膜の洗
浄法として一般的な水逆洗では除去できず、薬品洗浄を
行う必要がある。However, in recent years, TOC components composed of high molecular weight humic acid and fulvic acid, which are metabolites of microorganisms, have increased in raw water in water treatment due to organic contamination of industrial water and intake water sources of sewers. . For this reason, in the system for performing the pretreatment by such a membrane separation treatment, the polymeric humic acid or fulvic acid, which is the TOC component in the raw water, is not adsorbed on the surface of the MF or UF membrane for the pretreatment. The tendency to deposit and contaminate the membrane and increase the filtration resistance of the membrane is increasing. When film contamination by such polymeric humic acid or fulvic acid occurs, it cannot be removed by water backwashing as a general method for cleaning the MF film or UF film, and it is necessary to perform chemical cleaning.
【０００５】また、排水処理設備において、下水や産業
排水の生物処理水を処理して再利用する場合において
も、その生物処理水中には微生物代謝産物であるフミン
酸やフルボ酸からなるＴＯＣ成分が存在するため、上記
と同様な問題があった。[0005] Further, in the case of treating and recycling biologically treated water such as sewage or industrial wastewater in a wastewater treatment facility, TOC components comprising humic acid and fulvic acid, which are microbial metabolites, are contained in the biologically treated water. Due to the presence, there was the same problem as above.
【０００６】本発明者は、このような原水中のＴＯＣ成
分である高分子状のフミン酸やフルボ酸によるＭＦ膜や
ＵＦ膜の膜汚染の問題を解決すべく研究を重ねた結果、
これらの膜の前段でオゾン処理を実施することにより、
膜汚染を防止することができることを見出した。即ち、
オゾン処理によりこれら高分子状のフミン酸やフルボ酸
を分解することにより、原水中の高分子成分を減少させ
てＭＦ膜やＵＦ膜の有機物汚染を抑制させることができ
る。また、オゾン共存下でＭＦ膜やＵＦ膜に通水するこ
とにより、膜面に沈着したこれらの汚染物を酸化分解さ
せることもでき、常に清浄な膜面を保つことで、膜の透
過流束を高く維持することができる。The present inventor has conducted studies to solve the problem of membrane contamination of MF and UF membranes caused by such polymeric humic acid and fulvic acid as TOC components in raw water.
By performing ozone treatment before these films,
It has been found that membrane contamination can be prevented. That is,
By decomposing these polymeric humic acids and fulvic acids by ozone treatment, it is possible to reduce the amount of the polymeric components in the raw water and to suppress organic contamination of the MF film and the UF film. In addition, by passing water through the MF membrane or UF membrane in the coexistence of ozone, these contaminants deposited on the membrane surface can be oxidized and decomposed. Can be kept high.
【０００７】しかして、本発明者はこのようなオゾン共
存下でＭＦ膜やＵＦ膜に通水する装置において、より一
層安定かつ効率的な処理を行うべく、膜の透過水の残留
オゾン濃度を検出し、その値に基いてオゾン注入量を制
御する方式を先に提案した（特願平１０−８６１００
号）。[0007] However, the inventor of the present invention has proposed an apparatus for passing water through an MF membrane or a UF membrane in the presence of ozone to reduce the residual ozone concentration in the permeated water of the membrane in order to perform a more stable and efficient treatment. A method for detecting and controlling the ozone injection amount based on the detected value has been previously proposed (Japanese Patent Application No. 10-86100).
issue).
【０００８】[0008]
【発明が解決しようとする課題】このようにオゾンを注
入してオゾンにより原水中のＴＯＣ成分を酸化分解する
場合、具体的なオゾンの注入方法としては、膜分離装置
の前段にオゾン反応塔を設ける方法や、膜分離装置への
原水導入部に直接オゾンガスを供給する方法などが考え
られるが、それぞれ一長一短があり、必ずしも満足し得
るものではない。In the case of injecting ozone and oxidizing and decomposing the TOC component in the raw water with ozone as described above, a specific method of injecting ozone is to use an ozone reaction tower in front of the membrane separation apparatus. Although a method of providing the ozone gas and a method of directly supplying ozone gas to the raw water introduction section to the membrane separation device are conceivable, each method has advantages and disadvantages, and is not always satisfactory.
【０００９】即ち、膜分離装置の前段にオゾン反応塔を
設ける方法では、オゾン酸化時間を十分に確保すること
ができるため、原水中のＴＯＣ成分である高分子状のフ
ミン酸やフルボ酸の分解効率が高いが、オゾン反応塔を
必要とし、装置設備が大型化する。In other words, in the method in which the ozone reaction tower is provided in the preceding stage of the membrane separation device, since the ozone oxidation time can be sufficiently secured, the decomposition of the polymeric humic acid or fulvic acid, which is the TOC component in the raw water, is performed. Although high in efficiency, it requires an ozone reaction tower and the equipment becomes larger.
【００１０】また、膜分離装置への原水導入部に直接オ
ゾンガスを供給する方法では、オゾン反応塔は不要であ
るが、オゾン酸化時間が短く、原水中のＴＯＣ成分の分
解が不十分となり、後段の設備、例えば活性炭吸着塔の
負荷を増大するなどの問題がある。Further, in the method of directly supplying ozone gas to the raw water introduction section into the membrane separation apparatus, an ozone reaction tower is unnecessary, but the ozone oxidation time is short, and the decomposition of the TOC component in the raw water becomes insufficient. However, there is a problem such as an increase in the load of the equipment, for example, the activated carbon adsorption tower.
【００１１】本発明は上記従来の問題点を解決し、膜汚
染の防止のために原水をオゾン酸化処理した後、膜分離
処理する用排水処理装置において、オゾン反応塔を設け
ることなく、オゾンの吸収効率及びオゾンによる原水中
のＴＯＣ成分の酸化分解効率を高め、長期に亘り膜分離
装置を安定かつ効率的に運転することができる用排水処
理装置を提供することを目的とする。The present invention solves the above-mentioned conventional problems. In a wastewater treatment apparatus for subjecting raw water to an ozone oxidation treatment to prevent membrane contamination, and then performing a membrane separation treatment, an ozone reaction tower is not provided. An object of the present invention is to provide a wastewater treatment apparatus capable of increasing the absorption efficiency and the oxidative decomposition efficiency of TOC components in raw water by ozone, and stably and efficiently operating a membrane separation device for a long period of time.
【００１２】[0012]
【課題を解決するための手段】本発明の用排水処理装置
は、原水槽と、膜分離装置と、オゾン注入手段とを備え
た用排水処理装置であって、該オゾン注入手段は、原水
槽から膜分離装置へ原水を送給するための原水送給配管
と、膜分離装置の濃縮水を原水槽に戻すための濃縮水戻
り配管とにオゾンを供給可能であることを特徴とする。The wastewater treatment apparatus according to the present invention is a wastewater treatment apparatus comprising a raw water tank, a membrane separation device, and an ozone injection means, wherein the ozone injection means comprises a raw water tank. Ozone can be supplied to a raw water supply pipe for feeding raw water from the membrane separation device to the membrane separation device, and a concentrated water return piping for returning concentrated water of the membrane separation device to the raw water tank.
【００１３】本発明の用排水処理装置では、オゾンガス
を原水送給配管及び濃縮水戻り配管に直接注入すること
により次のような作用が奏される。これにより、オゾン
反応塔を設けることなくオゾンの吸収効率及びオゾンに
よるＴＯＣ成分の酸化分解効率を高めることができる。In the wastewater treatment apparatus of the present invention, the following operation is achieved by directly injecting ozone gas into the raw water supply pipe and the concentrated water return pipe. Thereby, the ozone absorption efficiency and the oxidative decomposition efficiency of the TOC component by ozone can be increased without providing an ozone reaction tower.
【００１４】 原水送給配管に直接オゾンガスを注入
すると共に、濃縮水戻り配管でもオゾンガスを注入する
ことにより、オゾンガスを原水槽にて再吸収させること
ができる。 膜分離装置で必須な逆洗操作等、原水が膜分離装置
に供給されない工程ないし期間において、オゾンガスの
供給を停止することなく、オゾン注入点を切り換え、濃
縮水戻り配管にオゾンガスを注入することにより、膜分
離処理の運転停止中もオゾンによる酸化分解を継続させ
ることができる。 上記より、膜分離処理を再開した時点で、原水の
オゾン酸化が進行しており、膜汚染物質である高分子状
のフミン酸やフルボ酸の分解が進んだ原水を膜分離装置
に供給できるため、膜汚染を低減させることができる。 逆洗工程等で膜面のフラッシングを原水を用いて行
う場合にも、逆洗工程中にオゾンガスが原水槽に供給さ
れ、原水のオゾン酸化を進行させることとなるため、フ
ラッシング原水からの膜面の汚染を防止することができ
る。 有機物濃度が高く、オゾン消費量が大きい原水を対
象とし、オゾン注入量を増加させる必要がある場合で
も、原水送給配管と濃縮水戻り配管との両方にオゾンガ
スを注入することで容易に対処できる。By injecting ozone gas directly into the raw water supply pipe and also injecting ozone gas into the concentrated water return pipe, the ozone gas can be reabsorbed in the raw water tank. By switching the ozone injection point and injecting ozone gas into the concentrated water return pipe without stopping the supply of ozone gas during the process or period in which raw water is not supplied to the membrane separation device, such as the backwashing operation required for the membrane separation device. In addition, the oxidative decomposition by ozone can be continued even while the operation of the membrane separation process is stopped. From the above, at the time when the membrane separation process is restarted, the ozone oxidation of the raw water is progressing, and the raw water in which the decomposition of high molecular weight humic acid and fulvic acid, which are the membrane contaminants, can be supplied to the membrane separation device. In addition, film contamination can be reduced. Even when the membrane surface is flushed with raw water in the backwashing step or the like, ozone gas is supplied to the raw water tank during the backwashing step and the ozone oxidation of the raw water proceeds, so that the membrane surface from the flushing raw water is used. Pollution can be prevented. Even if it is necessary to increase the amount of injected ozone for raw water with a high organic matter concentration and large ozone consumption, it can be easily dealt with by injecting ozone gas into both the raw water supply pipe and the concentrated water return pipe. .
【００１５】本発明の用排水処理装置では、濃縮水戻り
配管の末端は、原水槽内の保有原水中に位置することが
好ましく、これにより、原水槽をオゾン反応槽として機
能させてより一層オゾンの吸収効率を高めることができ
る。[0015] In the wastewater treatment apparatus of the present invention, the end of the concentrated water return pipe is preferably located in the raw water retained in the raw water tank, whereby the raw water tank functions as an ozone reaction tank to further reduce ozone. Absorption efficiency can be increased.
【００１６】[0016]
【発明の実施の形態】以下に図面を参照して本発明の実
施の形態を詳細に説明する。Embodiments of the present invention will be described below in detail with reference to the drawings.
【００１７】図１は本発明の用排水処理装置の実施の形
態を示す系統図である。FIG. 1 is a system diagram showing an embodiment of the wastewater treatment apparatus of the present invention.
【００１８】この用排水処理装置で原水の処理を行うに
は、バルブＶ1を開、バルブＶ2を閉としてポンプＰを作
動させる。配管１１より導入された原水は、原水槽１を
経て配管（原水送給配管）１２より膜分離装置２に導入
され、不溶物が固液分離される。この膜分離装置２の濃
縮水は循環水として配管（濃縮水戻り配管）１３より原
水槽１に戻され、透過水は処理水として配管１４より取
り出される。[0018] To perform the processing of raw water by the use waste water treatment apparatus, the valve V 1 opened, actuating the pump P and the valve V 2 is closed. The raw water introduced from the pipe 11 passes through the raw water tank 1 and is introduced into the membrane separation device 2 from the pipe (raw water supply pipe) 12 to separate insolubles into solid and liquid. The concentrated water from the membrane separation device 2 is returned to the raw water tank 1 from a pipe (concentrated water return pipe) 13 as circulating water, and the permeated water is taken out from a pipe 14 as treated water.
【００１９】このような膜分離処理において、オゾン発
生器３からのオゾンガスが配管３Ａ，３Ｂより配管１２
及び配管１３にそれぞれ注入されており、原水は配管１
２において膜分離処理に先立ちオゾンガスが注入され、
膜分離処理後、オゾンガスが注入された濃縮水が原水槽
１に循環される過程で更にオゾンガスが注入されること
で、効率的なオゾンの吸収及びＴＯＣ成分の酸化分解が
行われる。In such a membrane separation process, the ozone gas from the ozone generator 3 is supplied from the pipes 3A and 3B to the pipe 12
, And the raw water is supplied to the pipe 1.
In step 2, ozone gas is injected prior to the membrane separation process,
After the membrane separation treatment, the ozone gas is further injected in the course of circulating the concentrated water into which the ozone gas has been injected into the raw water tank 1, whereby efficient ozone absorption and oxidative decomposition of the TOC component are performed.
【００２０】原水送給配管である配管１２にオゾンガス
を注入する位置は、図示の如く、原水ポンプＰの入口側
とするのが、オゾンガスの注入効率の面で好ましい。ま
た、同様にオゾンガスの注入効率の面から、濃縮水戻り
配管である配管１３にオゾンガスを注入する位置は、図
示の如く、原水槽１に直結する垂直配管部分とするのが
好ましい。It is preferable that the ozone gas is injected into the raw water supply pipe 12 at the inlet side of the raw water pump P as shown in view of the ozone gas injection efficiency. Similarly, from the viewpoint of ozone gas injection efficiency, the position where the ozone gas is injected into the pipe 13 which is the concentrated water return pipe is preferably a vertical pipe portion directly connected to the raw water tank 1 as shown in the figure.
【００２１】図示の用排水処理装置では、この配管１３
の排出側の先端は原水槽１の保有原水中で開口してい
る。このように配管１３の開口を原水槽１の保有原水中
に設けることにより、原水槽１をオゾン反応塔として機
能させることができ、好ましい。In the illustrated waste water treatment apparatus, this pipe 13
Is open in the raw water held in the raw water tank 1. By providing the opening of the pipe 13 in the raw water held in the raw water tank 1, the raw water tank 1 can function as an ozone reaction tower, which is preferable.
【００２２】なお、原水槽をオゾン反応塔として機能さ
せる場合、原水槽は、その上部にラシヒリング等の充填
層を設け、この充填層の上方に散水機構を設けた構成と
しても良い。In the case where the raw water tank functions as an ozone reaction tower, the raw water tank may be provided with a packed layer such as a Raschig ring on the upper part thereof and a water spray mechanism provided above the packed layer.
【００２３】ところで、膜分離装置２では、膜分離処理
を継続して行うことにより膜面に汚染物が付着して膜の
透過流束が低下してくる。この場合には、ポンプＰを停
止して、自動弁Ｖ1を閉、自動弁Ｖ2を開とし、逆洗水を
配管１５より膜分離装置２に導入して配管１６より逆洗
排水を排出することにより膜面の逆流洗浄を行う。この
逆洗期間中は、オゾンガスを配管１３にのみ注入し、原
水槽１にオゾンガスを供給することで、逆洗期間中にお
いてもオゾンの吸収及びＴＯＣ成分の酸化分解を促進す
ることができる。By the way, in the membrane separation apparatus 2, by continuously performing the membrane separation process, contaminants adhere to the membrane surface, and the permeation flux of the membrane decreases. In this case, the pump P is stopped, closing the automatic valve V 1, and the automatic valve V 2 is opened, discharging the backwash effluent from the pipe 16 by introducing the backwash water to the membrane separation device 2 from the pipe 15 By doing so, backwashing of the membrane surface is performed. During the backwashing period, ozone gas is injected only into the pipe 13 and the ozone gas is supplied to the raw water tank 1, whereby the absorption of ozone and the oxidative decomposition of the TOC component can be promoted even during the backwashing period.
【００２４】また、原水中のＴＯＣ成分量が少ない場合
には、膜分離処理工程においては、原水送給配管である
配管１２にのみオゾンガスを注入し、逆洗工程において
は濃縮水戻り配管である配管１３にのみオゾンガスを注
入するようにオゾンガス注入点を切り換えても良い。こ
の場合、オゾンガスを注入する配管３Ａ，３Ｂの分岐点
に切り換え用の自動弁を設け、自動的にオゾン注入点を
切り換えるようにすることもできる。When the amount of the TOC component in the raw water is small, the ozone gas is injected only into the raw water supply pipe 12 in the membrane separation process, and the concentrated water return pipe is used in the backwashing step. The ozone gas injection point may be switched so that the ozone gas is injected only into the pipe 13. In this case, an automatic valve for switching may be provided at the branch point of the pipes 3A and 3B for injecting the ozone gas, and the ozone injection point may be automatically switched.
【００２５】なお、膜分離装置２の膜種としては、ＭＦ
膜、ＵＦ膜等を用いることができ、本発明においては、
図１に示す如く濃縮水の循環経路を有するクロスフロー
方式で処理を行う。The membrane type of the membrane separation device 2 is MF
A membrane, a UF membrane or the like can be used. In the present invention,
As shown in FIG. 1, the treatment is performed by a cross-flow method having a circulation path of the concentrated water.
【００２６】この膜分離装置２には、オゾンガスを含む
水が流入するため、膜分離装置２の膜の材質としては、
ガラスやアルミナ系のセラミック素材、金属製素材から
構成される無機膜や、有機膜にあっては、四フッ化ポリ
エチレンや二フッ化ポリビニリデン等のフッ素系素材や
ポリエーテルエーテルケトン等のオゾン耐食性の強いも
のを用いるのが好ましい。Since water containing ozone gas flows into the membrane separation device 2, the material of the membrane of the membrane separation device 2 is as follows.
For inorganic and organic films composed of glass, alumina-based ceramic materials and metal materials, ozone corrosion resistance of fluorine-based materials such as polyethylene tetrafluoride and polyvinylidene difluoride and polyetheretherketone Is preferably used.
【００２７】膜分離装置２の透過水は、残留オゾンの除
去、その他、膜分離装置２で除去し得なかった残留不純
物の除去を目的として、更に活性炭吸着塔に通水して処
理しても良い。The permeated water of the membrane separator 2 may be further passed through an activated carbon adsorption tower to remove residual ozone and other residual impurities that could not be removed by the membrane separator 2. good.
【００２８】[0028]
【発明の効果】以上詳述した通り、本発明の用排水処理
装置によれば、膜汚染の防止のために原水をオゾン酸化
処理した後、膜分離処理する用排水処理装置において、
オゾン反応塔を設けることなく、オゾンを原水に効率的
に吸収させて、オゾンによる原水中のＴＯＣ成分の酸化
分解効率を高め、安定かつ効率的な膜分離装置の運転を
長期に亘り継続して行うことができる。As described in detail above, according to the wastewater treatment apparatus of the present invention, in the wastewater treatment apparatus for subjecting raw water to ozone oxidation treatment to prevent membrane contamination and then performing membrane separation treatment,
Without providing an ozone reaction tower, ozone is efficiently absorbed in raw water, the efficiency of oxidative decomposition of TOC components in raw water by ozone is increased, and stable and efficient operation of the membrane separation device is continued for a long time. It can be carried out.
【図１】本発明の用排水処理装置の実施の形態を示す系
統図である。FIG. 1 is a system diagram showing an embodiment of a wastewater treatment apparatus of the present invention.
１ 原水槽 ２ 膜分離装置 ３ オゾン発生器 1 Raw water tank 2 Membrane separation device 3 Ozone generator
Claims (2)
段とを備えた用排水処理装置であって、 該オゾン注入手段は、原水槽から膜分離装置へ原水を送
給するための原水送給配管と、膜分離装置の濃縮水を原
水槽に戻すための濃縮水戻り配管とにオゾンを供給可能
であることを特徴とする用排水処理装置。1. A wastewater treatment apparatus provided with a raw water tank, a membrane separation device, and an ozone injection means, wherein the ozone injection means feeds raw water from the raw water tank to the membrane separation apparatus. A wastewater treatment apparatus characterized in that ozone can be supplied to a supply pipe and a concentrated water return pipe for returning concentrated water of a membrane separation device to a raw water tank.
有原水中に位置していることを特徴とする請求項１に記
載の用排水処理装置。2. The wastewater treatment apparatus according to claim 1, wherein an end of the concentrated water return pipe is located in raw water held in a raw water tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11111199A JP3707293B2 (en) | 1999-04-19 | 1999-04-19 | Wastewater treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11111199A JP3707293B2 (en) | 1999-04-19 | 1999-04-19 | Wastewater treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2000301174A true JP2000301174A (en) | 2000-10-31 |
| JP3707293B2 JP3707293B2 (en) | 2005-10-19 |
Family
ID=14552699
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11111199A Expired - Fee Related JP3707293B2 (en) | 1999-04-19 | 1999-04-19 | Wastewater treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3707293B2 (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003340469A (en) * | 2002-05-30 | 2003-12-02 | Ngk Insulators Ltd | Water treatment apparatus |
| JP2003340473A (en) * | 2002-05-30 | 2003-12-02 | Ngk Insulators Ltd | Water treatment apparatus |
| JP2012139659A (en) * | 2011-01-05 | 2012-07-26 | Kurita Water Ind Ltd | Treatment method and treatment apparatus of organic-matter-containing water |
| JP2018113925A (en) * | 2017-01-19 | 2018-07-26 | オルガノ株式会社 | Water treatment apparatus, water treatment method, and device for producing aquatic life rearing water |
-
1999
- 1999-04-19 JP JP11111199A patent/JP3707293B2/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003340469A (en) * | 2002-05-30 | 2003-12-02 | Ngk Insulators Ltd | Water treatment apparatus |
| JP2003340473A (en) * | 2002-05-30 | 2003-12-02 | Ngk Insulators Ltd | Water treatment apparatus |
| JP2012139659A (en) * | 2011-01-05 | 2012-07-26 | Kurita Water Ind Ltd | Treatment method and treatment apparatus of organic-matter-containing water |
| JP2018113925A (en) * | 2017-01-19 | 2018-07-26 | オルガノ株式会社 | Water treatment apparatus, water treatment method, and device for producing aquatic life rearing water |
| JP6996846B2 (en) | 2017-01-19 | 2022-01-17 | オルガノ株式会社 | Water treatment equipment, water treatment methods, and equipment for producing breeding water for aquatic organisms |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3707293B2 (en) | 2005-10-19 |
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