JP3449247B2 - Water treatment method and apparatus - Google Patents
Water treatment method and apparatusInfo
- Publication number
- JP3449247B2 JP3449247B2 JP28270498A JP28270498A JP3449247B2 JP 3449247 B2 JP3449247 B2 JP 3449247B2 JP 28270498 A JP28270498 A JP 28270498A JP 28270498 A JP28270498 A JP 28270498A JP 3449247 B2 JP3449247 B2 JP 3449247B2
- Authority
- JP
- Japan
- Prior art keywords
- ozone
- tank
- water
- membrane
- membrane filtration
- 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.)
- Expired - Fee Related
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- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、上水道、下水道、
工業用水または廃水処理の水処理方法およびその装置に
関し、詳しくはオゾン処理と膜ろ過処理を組み合わせ
て、膜ろ過処理効率が高く、しかもオゾン処理の効果が
高い水処理方法およびその装置に関するものである。TECHNICAL FIELD The present invention relates to a water supply system, a sewer system,
The present invention relates to a water treatment method and apparatus for industrial water or wastewater treatment, and more particularly to a water treatment method and apparatus having a high membrane filtration treatment efficiency and a high ozone treatment effect by combining ozone treatment and membrane filtration treatment. .
【０００２】[0002]
【従来の技術】従来、膜ろ過装置による水処理では、水
中の溶解性有機物を除去する目的で、生物処理、オゾン
処理、活性炭処理のような高度処理装置を前処理装置あ
るいは後処理装置として組み合わせた処理法が実施され
ている。2. Description of the Related Art Conventionally, in water treatment using a membrane filtration device, a high-level treatment device such as biological treatment, ozone treatment, activated carbon treatment is combined as a pretreatment device or a post-treatment device for the purpose of removing soluble organic substances in water. Different treatment methods are implemented.
【０００３】上水道における水処理では、原水中の溶解
性有機物であるトリハロメタン前駆物質や臭気物質を除
去するために、膜ろ過処理にオゾン処理と活性炭処理と
を付加することが有効である。オゾン処理では、原水中
の有機物を生物易分解性有機物に変えることが可能であ
り、オゾン処理によって後段の活性炭処理による有機物
の除去率が向上する。また、オゾン処理により溶存酸素
が過飽和になるために、後段の活性炭処理が生物処理能
力を持った生物活性炭となり、活性炭処理による有機物
等の除去率を長期に渡って維持することができ、活性炭
の交換コストを低減することができる。この原水のオゾ
ン処理では、副生成物が生成されるために、後段の活性
炭処理による副生成物の除去は不可欠である。因みに、
水道施設設計指針・解説（１９９０版）によれば、浄水
処理においてオゾン処理が用いられた場合は、活性炭処
理を併用しなければならないことが掲載されている。[0003] In water treatment in waterworks, it is effective to add ozone treatment and activated carbon treatment to the membrane filtration treatment in order to remove trihalomethane precursors and odor substances which are soluble organic substances in raw water. In the ozone treatment, organic matter in raw water can be converted into biodegradable organic matter, and the ozone treatment improves the removal rate of organic matter by the activated carbon treatment in the latter stage. Further, since the dissolved oxygen is supersaturated by the ozone treatment, the activated carbon treatment in the latter stage becomes a biological activated carbon having a biological treatment capacity, and the removal rate of organic matters and the like by the activated carbon treatment can be maintained for a long period of time. The replacement cost can be reduced. In this ozone treatment of raw water, by-products are produced, so removal of by-products by the subsequent treatment with activated carbon is indispensable. By the way,
According to the water supply facility design guide and explanation (1990 edition), when ozone treatment is used in water purification treatment, activated carbon treatment must be used together.
【０００４】通常、オゾン処理を用いた浄水処理では、
水処理の組み合わせとして、以下の２方式が主な処理フ
ローであった。その処理フローは、オゾン処理→活性
炭処理→膜ろ過処理と、膜ろ過処理→オゾン処理→活
性炭処理である。の処理方式は、原水にオゾンを直接
注入してオゾン処理した後に、活性炭処理を行って、最
後に膜ろ過処理を行い懸濁物質及び細菌類を除去するも
のである。この場合は、原水に直接オゾンが注入される
ため、オゾンの注入率が大きくなり経済的でない。の
処理方式は、膜ろ過処理で懸濁物質及び細菌類を除去し
た後に、オゾン処理および活性炭処理により有機物質等
を除去するものである。この場合は、原水を直接膜ろ過
処理するため、膜の目詰まりの進行が早いという問題が
ある。なお、およびの処理方式とも凝集沈殿処理あ
るいは凝集処理を前処理として付加することができる
が、膜ろ過による懸濁物質除去性能を生かすことができ
なくなるために望ましくない。Normally, in the water purification process using ozone treatment,
As the combination of water treatment, the following two methods were the main treatment flows. The processing flow is ozone treatment → activated carbon treatment → membrane filtration treatment and membrane filtration treatment → ozone treatment → activated carbon treatment. In the treatment method of 1, the ozone is directly injected into the raw water to perform the ozone treatment, the activated carbon treatment is performed, and finally the membrane filtration treatment is performed to remove suspended substances and bacteria. In this case, since ozone is directly injected into the raw water, the ozone injection rate becomes large, which is not economical. The treatment method of (1) is to remove organic substances and the like by ozone treatment and activated carbon treatment after removing suspended substances and bacteria by membrane filtration treatment. In this case, since the raw water is directly subjected to the membrane filtration treatment, there is a problem that the clogging of the membrane progresses quickly. In addition, both the treatment methods of and can add coagulation-sedimentation treatment or coagulation treatment as a pretreatment, but this is not preferable because the ability to remove suspended matter by membrane filtration cannot be utilized.
【０００５】一方、膜ろ過装置では、膜ろ過を継続して
いくと膜の目詰まりが起り、定期的に薬品洗浄を行って
膜のろ過性能を回復させなければならない。これらの問
題点を解決するために、従来例１の水処理装置では、図
６に示すように、被処理水をオゾン溶解槽兼接触槽１に
送り込んでオゾン酸化処理を行って、循環槽または膜供
給槽３に供給して、膜供給ポンプ５から膜ろ過装置６に
送り込み、その膜ろ過水を活性炭処理装置（または、活
性炭塔）８に送り込んでいる。このように、膜ろ過の前
にオゾン接触槽を設けて、膜ろ過する方法によって膜の
目詰まりを解消する処理方法が考えられた。しかし、こ
の処理方式の場合は以下のような問題点がある。先ず、
原水に対して直接オゾンを注入して反応させるため、オ
ゾン注入率を大きくしなければならず経済的ではない。
また、オゾン注入率を大きくすることにより副生成物を
生じ、後段の活性炭に対する負荷が大きくなる欠点があ
る。On the other hand, in the membrane filtration device, when the membrane filtration is continued, the membrane is clogged, and it is necessary to periodically perform chemical cleaning to recover the membrane filtration performance. In order to solve these problems, in the water treatment device of Conventional Example 1, as shown in FIG. 6, the water to be treated is sent to the ozone dissolution tank / contact tank 1 to carry out ozone oxidation treatment, and the circulation tank or It is supplied to the membrane supply tank 3, sent from the membrane supply pump 5 to the membrane filtration device 6, and the membrane filtration water is sent to the activated carbon treatment device (or activated carbon tower) 8. Thus, a treatment method has been considered in which an ozone contact tank is provided before membrane filtration and the membrane is clogged by a membrane filtration method. However, this processing method has the following problems. First,
Since ozone is directly injected into the raw water for reaction, the ozone injection rate must be increased, which is not economical.
In addition, there is a drawback that by-product is generated by increasing the ozone injection rate and the load on the activated carbon in the latter stage is increased.
【０００６】さらに、特開平１０−１１３６５９号公報
（以下、従来例２）には、図７に示すように、膜ろ過の
前でオゾンを注入して膜ろ過する方法が示されている。
被処理水が循環槽または膜供給水槽３に供給され、凝集
剤注入ポンプ４から凝集剤が供給され、その処理水が膜
供給ポンプ５によって膜ろ過装置６に供給される。その
過程でオゾン発生器２からオゾンが注入されて膜ろ過さ
れる。７は循環ラインである。ろ過水は、オゾン接触槽
９に送り込まれて活性炭処理装置８でろ過水中のオゾン
副生成物等が除去されている。Further, Japanese Patent Laid-Open No. 10-113659 (hereinafter referred to as Conventional Example 2) discloses a method of injecting ozone before membrane filtration to perform membrane filtration as shown in FIG.
The water to be treated is supplied to the circulation tank or the membrane supply water tank 3, the coagulant is supplied from the coagulant injection pump 4, and the treated water is supplied to the membrane filtration device 6 by the membrane supply pump 5. In the process, ozone is injected from the ozone generator 2 and membrane filtration is performed. 7 is a circulation line. The filtered water is sent to the ozone contact tank 9 and the ozone by-product in the filtered water is removed by the activated carbon treatment device 8.
【０００７】この従来例２の処理方式では、以下のよう
な問題点がある。先ず、オゾンがインライン注入されて
いるため、オゾンと有機物等が反応するための接触時間
を十分に確保することができないまま膜ろ過装置６に供
給される。さらに、膜ろ過装置６では、定期的に膜供給
ポンプ５を停止して物理洗浄を行わねばならないが、オ
ゾナイザー（オゾン発生器２）の間欠運転を行うことは
難しく、物理洗浄の間、オゾンを無駄に消費しなけれは
ならない。The processing method of the second conventional example has the following problems. First, since ozone is in-line injected, it is supplied to the membrane filtration device 6 without being able to secure a sufficient contact time for the reaction of ozone and organic substances. Further, in the membrane filtration device 6, the membrane supply pump 5 has to be periodically stopped to perform the physical cleaning, but it is difficult to perform the intermittent operation of the ozonizer (ozone generator 2), and the ozone is removed during the physical cleaning. It must be wasted.
【０００８】さらに、従来例２では、膜ろ過装置６によ
る膜ろ過の前段でオゾンを注入して膜ろ過した後に、再
度オゾンをオゾン接触槽９に注入し、オゾン酸化反応を
触媒に通水する方法である。しかし、オゾンと有機物質
との反応においては、十分なオゾン濃度との接触時間が
必要であり、オゾンのインライン注入方式では、オゾン
と有機物質との接触時間を十分に確保することができな
い欠点がある。Further, in Conventional Example 2, after ozone is injected and membrane-filtered before the membrane filtration by the membrane filtration device 6, ozone is again injected into the ozone contact tank 9 to pass the ozone oxidation reaction to the catalyst. Is the way. However, in the reaction between ozone and an organic substance, a sufficient contact time with ozone concentration is necessary, and the in-line injection method of ozone has a drawback that the contact time between ozone and an organic substance cannot be sufficiently secured. is there.
【０００９】[0009]
【発明が解決しようとする課題】本発明は、上記のよう
な従来技術の問題点を克服しようとするものであり、膜
ろ過処理による安定した処理水量を確保し得るととも
に、オゾン処理の効果を十分に発揮して、オゾン注入率
の削減や副生成物の生成の抑制を可能とする水処理方法
またはその装置を提供することを目的としている。DISCLOSURE OF THE INVENTION The present invention is intended to overcome the problems of the prior art as described above, and it is possible to secure a stable amount of treated water by the membrane filtration treatment and to achieve the effect of ozone treatment. It is an object of the present invention to provide a water treatment method or an apparatus therefor which can be sufficiently exhibited to reduce the ozone injection rate and suppress the production of by-products.
【００１０】[0010]
【課題を解決するための手段】本発明は、上記課題を達
成するために、請求項１の発明は、オゾン酸化を利用し
た水処理方法において、膜ろ過装置の前段に、オゾン溶
解槽と前記オゾン溶解槽にオゾンを注入するオゾン注入
設備とを備え、前記膜ろ過装置からの膜ろ過水中に残留
する残留オゾン濃度が所定範囲内となるように、前記残
留オゾン濃度の測定値に基づいて、前記オゾン溶解槽に
供給されるオゾン注入量を調整するとともに、前記膜ろ
過装置の後段のオゾン溶解槽兼接触槽にオゾンを注入
し、膜ろ過水をオゾン接触させて水処理することを特徴
とする水処理方法である。この構成によれば、膜ろ過水
中の残留オゾン濃度を監視して、膜ろ過装置の前段で必
要最小限のオゾンを供給することによって、膜ろ過装置
の通水抵抗を高めることなく膜ろ過水を得ることができ
るとともに、オゾンの副生成物の生成を抑制することが
できる。仮に、原水のオゾン要求量が変動したとしても
最適な量に設定することができる。さらに、膜ろ過水を
オゾン接触槽で十分に接触させることができるので、オ
ゾンの酸化作用によって有機物を分解することができ
る。また、オゾン溶解槽兼接触槽には、残存オゾン濃度
に応じて、オゾンを注入すればよく、オゾン消費を抑制
することができる。In order to achieve the above-mentioned object, the present invention provides a water treatment method utilizing ozone oxidation, wherein the ozone dissolving tank and the above-mentioned ozone dissolving tank are provided before the membrane filtration device. An ozone injection facility for injecting ozone into an ozone dissolution tank is provided, so that the residual ozone concentration remaining in the membrane filtration water from the membrane filtration device falls within a predetermined range, based on the measured value of the residual ozone concentration, The ozone injection amount supplied to the ozone dissolution tank is adjusted, and ozone is injected into the ozone dissolution tank / contact tank in the latter stage of the membrane filtration device, and the membrane filtration water is brought into contact with ozone for water treatment. Water treatment method. According to this configuration, the residual ozone concentration in the membranous filtered water is monitored, and the minimum necessary ozone is supplied in the preceding stage of the membranous filtered device, so that the membranous filtered water is collected without increasing the water resistance of the membranous filtered device. In addition to being obtained, it is possible to suppress the production of ozone by-products. Even if the ozone demand amount of the raw water changes, it can be set to an optimum amount. Furthermore, since the membrane-filtered water can be sufficiently brought into contact with the ozone contact tank, organic substances can be decomposed by the oxidizing action of ozone. In addition, ozone may be injected into the ozone dissolution tank / contact tank depending on the residual ozone concentration, so that ozone consumption can be suppressed.
【００１１】また、請求項２の発明は、前記残留オゾン
濃度が、０．０５〜１．０ｍｇ／Ｌの範囲内となるよう
に、前記オゾン注入量を調整することを特徴とする請求
項１に記載の水処理方法である。この構成によれば、オ
ゾン供給量を上記の範囲内とするように監視することに
よって、オゾン消費量を必要最小限に抑制することがで
きる。Further, the invention of claim 2 is characterized in that the ozone injection amount is adjusted so that the residual ozone concentration is within a range of 0.05 to 1.0 mg / L. The water treatment method described in 1. According to this configuration, by monitoring the ozone supply amount within the above range, the ozone consumption amount can be suppressed to the necessary minimum.
【００１２】また、請求項３の発明は、前記オゾン注入
量の調整が、前記膜ろ過装置の膜ろ過出口に設置したオ
ゾン検出器により連続的に膜ろ過水の残留オゾン濃度を
測定し、前記膜ろ過水中の残留オゾン濃度が、０．０５
〜１．０ｍｇ／Ｌの範囲内となるように、前記残留オゾ
ン濃度の測定値に基づいて、前記オゾン注入量をフィー
ドバック制御し、前記残留オゾン濃度を前記範囲内に調
整することを特徴とする請求項１に記載の水処理方法で
ある。この構成によれば、膜ろ過水中の残留オゾン濃度
を測定して、残留オゾン濃度が上記範囲とすることによ
り、必要最小限のオゾンを供給して、オゾンの副生成物
の生成を抑制することができる。仮に、原水のオゾン要
求量が変動したとしても最適な量に設定することができ
る。また、上記オゾン検出器は、溶存オゾン濃度検知器
を含むものである。In the invention of claim 3, the ozone injection amount is adjusted by continuously measuring the residual ozone concentration of the membrane filtration water by an ozone detector installed at the membrane filtration outlet of the membrane filtration device. The residual ozone concentration in the membrane filtration water is 0.05
Based on the measured value of the residual ozone concentration, the amount of injected ozone is feedback-controlled so that the residual ozone concentration is within the range of 1.0 mg / L. The water treatment method according to claim 1. According to this configuration, the residual ozone concentration in the membrane-filtered water is measured, and when the residual ozone concentration is within the above range, the minimum necessary ozone is supplied and the generation of ozone by-products is suppressed. You can Even if the ozone demand amount of the raw water changes, it can be set to an optimum amount. Further, the ozone detector includes a dissolved ozone concentration detector.
【００１３】また、請求項４の発明は、前記膜ろ過装置
の前段に、オゾン溶解槽と前記オゾン溶解槽にオゾンを
注入するオゾン注入設備とを備え、前記オゾン溶解槽ま
たは前記オゾン注入設備から前記膜ろ過装置までのオゾ
ン滞留時間が５分以内であり、かつ前記オゾン溶解槽兼
接触槽における滞留時間が５分以上であることを特徴と
する請求項１〜３に記載の水処理方法である。この構成
によれば、ろ過水中に溶存する有機物とオゾンとの接触
時間を十分に確保することができるとともに、膜ろ過水
中の残存オゾン濃度が検出されているので、オゾン溶解
槽兼接触槽には必要量のオゾンを注入すればよく、オゾ
ン消費を抑制できる。膜ろ過処理装置の膜ろ過処理効率
を損なうことなく、膜ろ過水に溶存する有機物とオゾン
との接触時間、すなわち酸化反応時間を十分に確保する
ことができる。Further, the invention of claim 4 is provided with an ozone dissolving tank and an ozone injecting equipment for injecting ozone into the ozone dissolving tank, in front of the membrane filtering device. 4. The water treatment method according to claim 1, wherein the ozone retention time to the membrane filtration device is within 5 minutes, and the retention time in the ozone dissolution tank / contact tank is 5 minutes or more. is there. According to this configuration, the contact time between the organic matter dissolved in the filtered water and ozone can be sufficiently secured, and the residual ozone concentration in the membrane filtered water is detected. It is sufficient to inject a necessary amount of ozone, and it is possible to suppress ozone consumption. The contact time between the organic matter dissolved in the membrane filtration water and ozone, that is, the oxidation reaction time can be sufficiently secured without impairing the membrane filtration efficiency of the membrane filtration device.
【００１４】また、請求項５の発明は、オゾンを被処理
水に溶解して膜ろ過装置で膜ろ過し、そのろ過水をオゾ
ン溶解槽兼接触槽に送って水処理する水処理装置であっ
て、前記膜ろ過装置の前段に、オゾン溶解槽と前記オゾ
ン溶解槽にオゾンを注入するオゾン注入設備とを備え、
前記膜ろ過装置の膜ろ過出口に設置した膜ろ過水中の残
留オゾン濃度を計測するオゾン検出器と、前記オゾン検
出器によって膜ろ過水中の残留オゾン濃度を測定し、そ
の計測値に基づいて、前記オゾン溶解槽に供給されるオ
ゾン注入量を調整し、膜ろ過水中の残留オゾン濃度を所
定範囲内とするように制御する制御手段とを具備するこ
とを特徴とする水処理装置である。この構成によれば、
膜ろ過水に混入する残留オゾン濃度を必要最小限に抑制
することができ、膜の目詰まりが抑制できる。また、上
記オゾン検出器は、溶存オゾン濃度検知器を含むもので
ある。Further, the invention of claim 5 is a water treatment device for dissolving ozone in water to be treated, performing membrane filtration with a membrane filtration device, and sending the filtered water to an ozone dissolution tank / contact tank for water treatment. In the preceding stage of the membrane filtration device, an ozone dissolution tank and an ozone injection facility for injecting ozone into the ozone dissolution tank are provided,
An ozone detector that measures the residual ozone concentration in the membrane filtration water installed at the membrane filtration outlet of the membrane filtration device, and measure the residual ozone concentration in the membrane filtration water by the ozone detector, based on the measured value, A water treatment apparatus comprising: a control unit that adjusts an ozone injection amount supplied to an ozone dissolution tank and controls the residual ozone concentration in the membrane filtration water so as to be within a predetermined range. According to this configuration,
The residual ozone concentration mixed in the membrane filtered water can be suppressed to the necessary minimum, and the clogging of the membrane can be suppressed. Further, the ozone detector includes a dissolved ozone concentration detector.
【００１５】また、請求項６の発明は、前記膜ろ過装置
の前段に循環槽または膜供給槽を設け、前記循環槽また
は膜供給槽がオゾン溶解槽を兼ねることを特徴とする請
求項５に記載の水処理装置である。この構成によれば、
膜ろ過水に残留する残留オゾン濃度を最小限に制御され
ており、オゾンの効果を発揮し得る小型化された装置を
構成し得る。また、オゾンの滞留時間の制御が容易であ
る。Further, the invention of claim 6 is characterized in that a circulation tank or a membrane supply tank is provided in the preceding stage of the membrane filtration device, and the circulation tank or the membrane supply tank also serves as an ozone dissolution tank. It is the described water treatment device. According to this configuration,
The residual ozone concentration remaining in the membrane-filtered water is controlled to the minimum, and a miniaturized device that can exert the effect of ozone can be configured. Further, it is easy to control the residence time of ozone.
【００１６】また、請求項７の発明は、前記膜ろ過装置
の前段に、原水を受水する原水受水槽と循環槽または膜
供給槽とが設けられ、前記原水受水槽に凝集剤を供給
し、前記循環槽または膜供給槽にオゾンを供給するよう
にしたことを特徴とする請求項５または６に記載の水処
理装置である。この構成によれば、原水受水槽を凝集剤
処理槽と兼用するとともに、膜ろ過水に残留する残留オ
ゾン濃度が必要最小限に抑制され、オゾンとの接触時間
を維持し、オゾンの酸化反応による効果を発揮し得る小
型化された装置を構成し得る。また、オゾンの反応に必
要な滞留時間の制御が容易である。Further, in the invention of claim 7, a raw water receiving tank for receiving raw water and a circulation tank or a membrane supply tank are provided in front of the membrane filtration device, and a coagulant is supplied to the raw water receiving tank. 7. The water treatment device according to claim 5, wherein ozone is supplied to the circulation tank or the membrane supply tank. According to this configuration, the raw water receiving tank is also used as the coagulant treatment tank, the residual ozone concentration remaining in the membrane filtered water is suppressed to the necessary minimum, the contact time with ozone is maintained, and the ozone oxidation reaction A miniaturized device that can exert the effect can be configured. In addition, it is easy to control the residence time required for ozone reaction.
【００１７】[0017]
【発明の実施の形態】以下、本発明の水処理方法および
その装置について、図面を参照して詳細に説明する。図
１〜４は、それぞれ異なった実施形態を示す処理フロー
である。BEST MODE FOR CARRYING OUT THE INVENTION The water treatment method and apparatus of the present invention will be described below in detail with reference to the drawings. 1 to 4 are process flows showing different embodiments.
【００１８】（実施形態１）図１は、本発明の水処理方
法およびその装置の一実施形態を説明するための処理フ
ローを示す図である。同図において、被処理水は、オゾ
ン溶解槽１０に供給され、オゾン発生器２からオゾンが
オゾン溶解槽１０に注入され、オゾンが溶解した被処理
水は、循環槽または膜供給水槽３に送り込まれる。循環
槽３には、凝集剤注入ポンプ４から凝集剤を供給するこ
ともできる。循環槽３の膜ろ過供給水は、膜供給ポンプ
５によって、膜ろ過装置６に供給される。膜ろ過装置６
を透過した膜ろ過水は、オゾン溶解槽兼接触槽１１に送
り込まれる。オゾン溶解槽兼接触槽１１には、オゾン発
生器２から必要量のオゾンが供給されて膜ろ過水とオゾ
ンが接触する。膜ろ過水が膜ろ過装置６からオゾン溶解
槽兼接触槽１１に送り込まれる過程で、膜ろ過水中の残
留オゾン濃度がオゾン検出器１２で検出され、そのオゾ
ン濃度の計測値に基づいてオゾン発生器２からオゾン溶
解槽１０へのオゾン供給量が制御されている。オゾン溶
解槽兼接触槽１１で十分にオゾンと接触した膜ろ過水
は、活性炭処理装置（活性炭塔）８に送り込まれ、オゾ
ン副生成物等が活性炭に吸着されて、浄化された処理水
が得られる。また、オゾン溶解槽１０、循環槽３、オゾ
ン溶解槽兼接触槽１１からの排出される排オゾンは、排
オゾン処理設備１３で処理される。膜ろ過膜６からの循
環水は、循環ライン７を通して循環槽３や膜供給ポンプ
５の前に返送される。なお、以下の実施形態においても
同様であるが、オゾン検出器１２は、溶存オゾン濃度検
知器であってもよい。(Embodiment 1) FIG. 1 is a diagram showing a treatment flow for explaining an embodiment of a water treatment method and apparatus of the present invention. In the figure, the water to be treated is supplied to the ozone dissolving tank 10, ozone is injected from the ozone generator 2 into the ozone dissolving tank 10, and the water to be treated in which ozone is dissolved is sent to the circulation tank or the membrane supply water tank 3. Be done. The coagulant may be supplied from the coagulant injection pump 4 to the circulation tank 3. The membrane filtration supply water of the circulation tank 3 is supplied to the membrane filtration device 6 by the membrane supply pump 5. Membrane filtration device 6
The membrane-filtered water that has passed through is sent to the ozone dissolution tank / contact tank 11. A necessary amount of ozone is supplied from the ozone generator 2 to the ozone dissolution tank / contact tank 11, and the membrane filtered water and ozone come into contact with each other. In the process in which the membrane filtration water is sent from the membrane filtration device 6 to the ozone dissolution tank / contact tank 11, the residual ozone concentration in the membrane filtration water is detected by the ozone detector 12, and the ozone generator is generated based on the measured ozone concentration value. The amount of ozone supplied from 2 to the ozone dissolving tank 10 is controlled. The membrane-filtered water that has sufficiently contacted with ozone in the ozone dissolution tank / contact tank 11 is sent to the activated carbon treatment device (activated carbon tower) 8 and ozone by-products and the like are adsorbed on the activated carbon to obtain purified treated water. To be The waste ozone discharged from the ozone dissolution tank 10, the circulation tank 3, and the ozone dissolution tank / contact tank 11 is processed by the waste ozone treatment facility 13. The circulating water from the membrane filtration membrane 6 is returned to the front of the circulation tank 3 and the membrane supply pump 5 through the circulation line 7. The ozone detector 12 may be a dissolved ozone concentration detector, although the same applies to the following embodiments.
【００１９】本実施形態では、オゾン検出器１２によっ
て、膜ろ過水中の残留オゾン濃度が常時計測されてお
り、残留オゾン濃度が、０．１〜１．０ｍｇ／Ｌの範囲
となるように、オゾン発生器２からオゾン溶解槽１０へ
供給されるオゾン注入量がバルブの開閉操作によって調
整されている。そして、本水処理装置では、オゾンが供
給された槽から膜ろ過装置６までのオゾン滞留時間を５
分以内とし、オゾン溶解槽兼接触槽１１でのオゾン滞留
時間を５分以上とする。なお、以下の実施形態も同様で
あるが、オゾン発生器２やオゾンをオゾン溶解槽１０や
オゾン溶解槽兼接触槽１１に所定量のオゾンを供給する
ための設備を含めてオゾン注入設備と称する。In the present embodiment, the ozone detector 12 constantly measures the residual ozone concentration in the membrane-filtered water, so that the ozone concentration is in the range of 0.1 to 1.0 mg / L. The ozone injection amount supplied from the generator 2 to the ozone dissolution tank 10 is adjusted by opening / closing the valve. In the present water treatment device, the ozone retention time from the tank to which ozone is supplied to the membrane filtration device 6 is set to 5
Within 5 minutes, the ozone retention time in the ozone dissolution tank / contact tank 11 is set to 5 minutes or longer. Although the same applies to the following embodiments, the ozone generator 2 and equipment for supplying a predetermined amount of ozone to the ozone dissolution tank 10 and the ozone dissolution tank / contact tank 11 are referred to as ozone injection equipment. .
【００２０】（実施形態２）図２は、本発明の水処理方
法およびその装置の他の実施形態を説明するための処理
フローを示す図である。同図において、被処理水は、循
環槽兼オゾン溶解槽１４に供給され、かつオゾン発生器
２からオゾンが注入されている。さらに、この槽には、
凝集剤注入ポンプ４から凝集剤を供給することもでき
る。オゾンが溶解する膜ろ過供給水は、膜供給ポンプ５
によって、膜ろ過装置６に供給される。膜ろ過装置６を
透過した膜ろ過水は、オゾン溶解槽兼接触槽１１に送り
込まれる。膜ろ過装置６からオゾン溶解槽兼接触槽１１
に膜ろ過水が供給される過程で、膜ろ過水中の残留オゾ
ン濃度がオゾン検出器１２で検出され、そのオゾン濃度
の計測値に基づいてオゾン発生器２から循環槽兼オゾン
溶解槽１４へのオゾン供給量が制御されている。また、
オゾン発生器２からオゾン溶解槽兼接触槽１１にオゾン
が供給されており、膜ろ過水は、オゾン溶解槽兼接触槽
１１で十分にオゾンと接触して、活性炭処理装置８に送
り込まれて、オゾン副生成物等が活性炭に吸着され、浄
化された処理水が得られる。循環槽兼オゾン溶解槽１
４、オゾン溶解槽兼接触槽１１からの放出される排オゾ
ンは、排オゾン処理設備１３で処理される。(Embodiment 2) FIG. 2 is a diagram showing a treatment flow for explaining another embodiment of the water treatment method and apparatus of the present invention. In the figure, the water to be treated is supplied to the circulation tank and ozone dissolving tank 14, and ozone is injected from the ozone generator 2. Furthermore, in this tank,
The coagulant may be supplied from the coagulant injection pump 4. Membrane filtration supply water in which ozone is dissolved is the membrane supply pump 5
Is supplied to the membrane filtration device 6. The membrane filtered water that has passed through the membrane filtering device 6 is sent to the ozone dissolving tank / contact tank 11. From the membrane filtration device 6 to the ozone dissolution tank and contact tank 11
The residual ozone concentration in the membrane filtration water is detected by the ozone detector 12 during the process of supplying the membrane filtration water to the circulation tank and the ozone dissolving tank 14 from the ozone generator 2 based on the measured value of the ozone concentration. Ozone supply is controlled. Also,
Ozone is being supplied from the ozone generator 2 to the ozone dissolution tank / contact tank 11, the membrane filtered water is sufficiently contacted with ozone in the ozone dissolution tank / contact tank 11, and is sent to the activated carbon treatment device 8. By-products such as ozone are adsorbed on the activated carbon, and purified treated water is obtained. Circulation tank and ozone dissolution tank 1
4. The exhaust ozone discharged from the ozone dissolution tank / contact tank 11 is processed by the exhaust ozone processing facility 13.
【００２１】本実施形態では、オゾン検出器１２によっ
て、膜ろ過水中の残留オゾン濃度が計測されており、残
留オゾン濃度が上記範囲となるように、オゾン発生器２
から循環槽兼オゾン溶解槽１４へ供給されるオゾン注入
量がバルブの開閉操作によって調整されている。そし
て、本水処理装置では、オゾンが供給された槽またはオ
ゾン発生器２から膜ろ過装置６までのオゾン滞留時間を
５分以内とし、オゾン溶解槽兼接触槽１１でのオゾン滞
留時間を５分以上とする。In the present embodiment, the ozone detector 12 measures the residual ozone concentration in the membrane-filtered water, and the ozone generator 2 keeps the residual ozone concentration within the above range.
The amount of ozone injected from the circulating tank to the ozone dissolving tank 14 is adjusted by opening / closing the valve. In the present water treatment device, the ozone retention time from the ozone-supplied tank or ozone generator 2 to the membrane filtration device 6 is within 5 minutes, and the ozone retention time in the ozone dissolution tank / contact tank 11 is 5 minutes. That is all.
【００２２】（実施形態３）図３は、本発明の水処理方
法およびその装置の他の実施形態を説明するための処理
フローを示す図である。同図において、原水が原水受槽
１５に送り込まれ、この槽には凝集剤注入ポンプ４から
凝集剤が供給されている。原水受槽１５からの凝集処理
水は、オゾン発生器２からオゾンが供給されている循環
槽兼オゾン溶解槽１６に供給されて、膜供給ポンプ５に
よって、膜ろ過装置６に供給されている。膜ろ過装置６
を透過した膜ろ過水は、オゾン発生器２からオゾンが供
給されているオゾン溶解槽兼接触槽１１に送り込まれ
る。膜ろ過装置６からオゾン溶解槽兼接触槽１１へ膜ろ
過水が供給される過程で、膜ろ過水中の残留オゾン濃度
がオゾン検出器１２で検出され、その残留オゾン濃度の
計測値に基づいてオゾン発生器２から循環槽兼オゾン溶
解槽１６へのオゾン供給量が制御されて、膜ろ過水中の
残存オゾン濃度が所定範囲となるように制御されてい
る。オゾン溶解槽兼接触槽１１で十分にオゾンと接触し
た膜ろ過水は、活性炭処理装置８に送り込まれて、オゾ
ン副生成物等が活性炭に吸着されて、浄化された処理水
が得られる。循環槽兼オゾン溶解槽１６、オゾン溶解槽
兼接触槽１１からの放出される排オゾンは、排オゾン処
理設備１３で処理される。また、循環水は、循環ライン
７を通して原水受槽１５、循環槽兼オゾン溶解槽１６、
膜供給ポンプ５の前段に供給されている。(Embodiment 3) FIG. 3 is a diagram showing a treatment flow for explaining another embodiment of the water treatment method and apparatus of the present invention. In the figure, raw water is sent to a raw water receiving tank 15, and a coagulant is supplied from a coagulant injection pump 4 to this tank. The coagulated water from the raw water receiving tank 15 is supplied to the circulation tank / ozone dissolving tank 16 to which ozone is being supplied from the ozone generator 2, and is supplied to the membrane filtration device 6 by the membrane supply pump 5. Membrane filtration device 6
The membrane-filtered water that has passed through is sent to the ozone dissolution tank / contact tank 11 to which ozone is supplied from the ozone generator 2. During the process of supplying the membrane filtration water from the membrane filtration device 6 to the ozone dissolution tank / contact tank 11, the residual ozone concentration in the membrane filtration water is detected by the ozone detector 12, and the ozone is detected based on the measured value of the residual ozone concentration. The amount of ozone supplied from the generator 2 to the circulation tank / ozone dissolving tank 16 is controlled so that the residual ozone concentration in the membrane-filtered water falls within a predetermined range. The membrane-filtered water that has been sufficiently contacted with ozone in the ozone dissolution tank / contact tank 11 is sent to the activated carbon treatment device 8 where ozone by-products and the like are adsorbed on the activated carbon to obtain purified treated water. The exhaust ozone discharged from the circulation tank / ozone dissolution tank 16 and the ozone dissolution tank / contact tank 11 is processed by the exhaust ozone treatment facility 13. In addition, the circulating water is supplied through the circulation line 7 to the raw water receiving tank 15, the circulating tank and the ozone dissolving tank 16,
It is supplied to the front stage of the membrane supply pump 5.
【００２３】本実施形態では、オゾン検出器１２によっ
て、膜ろ過水中の残留オゾン濃度が計測されており、残
留オゾン濃度が上記範囲となるように、オゾン発生器２
から循環槽兼オゾン溶解槽１６へ供給されるオゾン注入
量がバルブの開閉操作によって調整されている。そし
て、本水処理装置では、オゾンが供給された槽またはオ
ゾン発生器２から膜ろ過装置６までのオゾン滞留時間を
５分以内とし、オゾン溶解槽兼接触槽１１でのオゾン滞
留時間を５分以上とする。In the present embodiment, the ozone detector 12 measures the residual ozone concentration in the membrane-filtered water, and the ozone generator 2 keeps the residual ozone concentration within the above range.
The ozone injection amount supplied from the circulating tank to the ozone dissolving tank 16 is adjusted by opening / closing the valve. In the present water treatment device, the ozone retention time from the ozone-supplied tank or ozone generator 2 to the membrane filtration device 6 is within 5 minutes, and the ozone retention time in the ozone dissolution tank / contact tank 11 is 5 minutes. That is all.
【００２４】（実施形態４）図４は、本発明の水処理方
法およびその装置の他の実施形態を説明するための処理
フローを示す図である。同図において、循環槽兼オゾン
溶解槽１４は、仕切壁で区分けされ、凝集剤注入ポンプ
４から凝集剤が供給される槽と、オゾン発生器２からオ
ゾンが供給される槽とに区分けられ、循環槽兼オゾン溶
解槽１４におけるオゾン溶解した循環水は、膜供給ポン
プ５によって、膜ろ過装置６に供給される。膜ろ過水
は、オゾン発生器２からオゾンが供給されているオゾン
溶解槽兼接触槽１１に送り込まれる。膜ろ過装置６から
オゾン溶解槽兼接触槽１１に送り込まれる過程で、膜ろ
過水中の残留オゾン濃度がオゾン検出器１２で検出さ
れ、そのオゾン濃度の計測値に基づいて、上記の範囲と
なるように、オゾン発生器２から循環槽兼オゾン溶解槽
１４へのオゾン供給量が制御されている。オゾン溶解槽
兼接触槽１１で十分にオゾンと接触した膜ろ過水は、活
性炭処理装置８に送り込まれて、オゾン副生成物等が活
性炭に吸着され、浄化された処理水が得られる。循環槽
兼オゾン溶解槽１４、オゾン溶解槽兼接触槽１１からの
排出される排オゾンは、排オゾン処理設備１３で処理さ
れる。(Embodiment 4) FIG. 4 is a diagram showing a treatment flow for explaining another embodiment of the water treatment method and apparatus of the present invention. In the figure, the circulation tank / ozone dissolving tank 14 is divided by a partition wall into a tank to which the coagulant is supplied from the coagulant injection pump 4 and a tank to which ozone is supplied from the ozone generator 2. The circulation water in which ozone is dissolved in the circulation tank / ozone dissolution tank 14 is supplied to the membrane filtration device 6 by the membrane supply pump 5. The membrane filtered water is sent from the ozone generator 2 to the ozone dissolution tank / contact tank 11 to which ozone is supplied. The residual ozone concentration in the membrane filtration water is detected by the ozone detector 12 in the process of being fed from the membrane filtration device 6 into the ozone dissolution tank / contact tank 11, and is set within the above range based on the measured value of the ozone concentration. In addition, the amount of ozone supplied from the ozone generator 2 to the circulation tank and ozone dissolution tank 14 is controlled. The membrane-filtered water that has been sufficiently contacted with ozone in the ozone dissolution tank / contact tank 11 is sent to the activated carbon treatment device 8 where ozone by-products and the like are adsorbed on the activated carbon to obtain purified treated water. The exhaust ozone discharged from the circulation tank / ozone dissolution tank 14 and the ozone dissolution tank / contact tank 11 is processed by the exhaust ozone treatment facility 13.
【００２５】本実施形態では、オゾン検出器１２によっ
て、膜ろ過水中の残留オゾン濃度が計測されており、残
留オゾン濃度が上記範囲となるように、オゾン発生器２
から循環槽兼オゾン溶解槽１４へ供給されるオゾン注入
量がバルブの開閉操作によって調整されている。そし
て、本水処理装置では、上記実施形態と同様にオゾンが
供給された槽から膜ろ過装置６までのオゾン滞留時間を
５分以内とし、オゾン溶解槽兼接触槽１１でのオゾン滞
留時間を５分以上とする。In this embodiment, the ozone detector 12 measures the residual ozone concentration in the membrane-filtered water, and the ozone generator 2 keeps the residual ozone concentration within the above range.
The amount of ozone injected from the circulating tank to the ozone dissolving tank 14 is adjusted by opening / closing the valve. Then, in the present water treatment device, the ozone retention time from the tank to which ozone is supplied to the membrane filtration device 6 is set to 5 minutes or less, and the ozone retention time in the ozone dissolution tank / contact tank 11 is 5 as in the above embodiment. It should be more than a minute.
【００２６】次に、本発明を示す上記実施形態１〜４の
各構成要素について、さらに詳細に説明する。なお、以
下の個々の要素説明によって、上記実施形態に基づく発
明に限定を加えるものではないが、下記の個々の記述に
は、本発明に付随する発明を包含している。Next, each component of the above-described first to fourth embodiments showing the present invention will be described in more detail. It should be noted that the following description of individual elements does not limit the invention based on the above-described embodiment, but the following individual descriptions include inventions associated with the present invention.
【００２７】（１）本発明のオゾン溶解槽について説明
する。上記実施形態では、オゾン溶解槽がオゾン溶解を
単独機能とするものと、オゾン溶解とそれ以外の循環槽
等との複合的機能を併せ持ったものとがある。図１の実
施形態では、被処理水（原水）を受水するが、オゾン溶
解槽１０を単独機能とし、循環槽３とは分離されてい
る。図２の実施形態では、循環槽兼オゾン溶解槽１４で
あり、凝集剤が混入される複合的機能を有するものであ
る。図３の実施形態では、循環槽を兼ねるオゾン溶解槽
である。凝集剤は原水受槽１５に供給されている。図４
の実施形態では、仕切壁が設けられて、被処理水（原
水）を受水するとともに、それぞれの区域に凝集剤の投
入とオゾンの溶解とを兼ね備える循環槽兼オゾン溶解槽
１４である。(1) The ozone dissolving tank of the present invention will be described. In the above-described embodiments, there are those in which the ozone dissolution tank has a single function of ozone dissolution, and those in which the ozone dissolution tank has a combined function of ozone dissolution and other circulation tanks. In the embodiment of FIG. 1, water to be treated (raw water) is received, but the ozone dissolving tank 10 has a single function and is separated from the circulation tank 3. In the embodiment of FIG. 2, it is the circulation tank and ozone dissolution tank 14, and has a complex function of mixing the coagulant. In the embodiment of FIG. 3, it is an ozone dissolving tank which also serves as a circulation tank. The coagulant is supplied to the raw water receiving tank 15. Figure 4
In the embodiment, the partition tank is provided to receive the water to be treated (raw water), and is a circulation tank / ozone dissolving tank 14 that both inputs a coagulant and dissolves ozone in each area.
【００２８】オゾン溶解槽の目的は、膜ろ過装置のろ過
速度を高く維持するために膜ろ過供給水にオゾンを溶解
させるためのものである。オゾン発生器２からオゾンが
オゾン溶解槽に注入され、膜ろ過装置６を通過した膜ろ
過水に残留する残量オゾン量は、膜ろ過装置６のろ過速
度を高く維持するために、０．０５〜１．０ｍｇ／Ｌと
し、望ましくは、０．２〜０．４ｍｇ／Ｌとするとよ
い。膜ろ過水の残留オゾン濃度が、０．４ｍｇ／Ｌより
高くなった場合、膜ろ過装置６のろ過膜として、耐オゾ
ン性の膜素材を用いても長期的にはオゾンとの反応によ
る膜劣化が起こる恐れがあるが、膜モジュールの交換時
期を考え合わせると、１．０ｍｇ／Ｌまでは許容され
る。また、オゾン注入量が１．０ｍｇ／Ｌより多くなる
と、副生成物量も多くなる問題がある。以上のことか
ら、膜ろ過水の残留オゾン濃度は、０．０５〜１．０ｍ
ｇ／Ｌとし、望ましくは、０．２〜０．４ｍｇ／Ｌとす
るとよい。The purpose of the ozone dissolution tank is to dissolve ozone in the membrane filtration feed water in order to maintain a high filtration rate of the membrane filtration device. Ozone is injected from the ozone generator 2 into the ozone dissolution tank, and the residual ozone amount remaining in the membrane filtration water that has passed through the membrane filtration device 6 is 0.05 in order to maintain a high filtration rate of the membrane filtration device 6. ˜1.0 mg / L, and preferably 0.2 to 0.4 mg / L. When the residual ozone concentration of the membrane filtration water is higher than 0.4 mg / L, even if an ozone resistant membrane material is used as the filtration membrane of the membrane filtration device 6, the membrane is deteriorated due to the reaction with ozone in the long term. However, considering the replacement timing of the membrane module, up to 1.0 mg / L is acceptable. Further, if the ozone injection amount exceeds 1.0 mg / L, there is a problem that the amount of by-products also increases. From the above, the residual ozone concentration of the membrane filtration water is 0.05 to 1.0 m.
g / L, and preferably 0.2 to 0.4 mg / L.
【００２９】なお、本実施形態では、膜ろ過の後段で膜
ろ過水をオゾンと再接触させているために、膜ろ過の前
段でオゾンと十分に接触させる必要はない。むしろ、濁
質が多く含まれている原水とオゾンとの接触時間を長く
した場合、濁質とオゾンとの反応によって、オゾンの消
費が多くなるので、オゾンを溶解させたら直ちに膜ろ過
することによって、濁質とオゾンとの反応によるオゾン
の消費を防止することができるとともに、膜ろ過装置６
の機能を十分に発揮させることができる。上記実施形態
では、原水とオゾンとの接触時間を５分以内としてい
る。In this embodiment, since the membrane-filtered water is brought into contact with ozone again after the membrane filtration, it is not necessary to sufficiently contact the ozone before the membrane filtration. Rather, if the contact time between raw water containing a large amount of suspended solids and ozone is lengthened, the ozone consumption will increase due to the reaction between the suspended solids and ozone, so use membrane filtration immediately after dissolving the ozone. The consumption of ozone due to the reaction between turbidity and ozone can be prevented, and the membrane filtration device 6
The function of can be fully exerted. In the above embodiment, the contact time between raw water and ozone is within 5 minutes.
【００３０】上記実施形態のように、単独または複合機
能を有するオゾン溶解槽がディフューザ形式の場合、瞬
時にオゾンを溶解することは不可能であり、ある程度滞
留時間を持たせることによって効率的にオゾンを溶解さ
せることができる。また、オゾン溶解槽におけるオゾン
接触効率は、滞留時間が短い場合は溶解効率が悪くなる
ので、オゾン消費量およびオゾン溶解効率を考慮して、
オゾン溶解槽及び循環槽における総接触時間は、５分以
内であることが望ましい。また、オゾン溶解槽の装置形
式は、Ｕチューブ式、ディフューザ式、インジェクタ
式、エジェクタ式、下降注入式注入等のどの形式でも可
能である。但し、オゾンを溶解させた後に、オゾンとの
接触時間を必要以上に取らない方式であることが望まし
い。すなわち、図１の実施形態は、通常の膜ろ過装置
（循環槽、膜供給ポンプ及び膜モジュールから構成され
る）の前段に、オゾン溶解槽を設けたものである。この
場合は、槽の容量をなるべく小さくして、オゾンとの接
触時間を取らないようにする。As in the above embodiment, when the ozone dissolving tank having a single function or a compound function is of the diffuser type, it is impossible to dissolve ozone instantly, and it is possible to efficiently retain ozone by giving a certain residence time. Can be dissolved. Further, regarding the ozone contact efficiency in the ozone dissolution tank, the dissolution efficiency becomes poor when the residence time is short, so in consideration of ozone consumption and ozone dissolution efficiency,
The total contact time in the ozone dissolution tank and the circulation tank is preferably within 5 minutes. Further, the ozone dissolving tank may be of any type such as a U tube type, a diffuser type, an injector type, an ejector type, and a downward injection type injection. However, it is desirable to adopt a method in which the contact time with ozone is not taken unnecessarily after the ozone is dissolved. That is, in the embodiment of FIG. 1, an ozone dissolving tank is provided in the preceding stage of a normal membrane filtration device (which is composed of a circulation tank, a membrane supply pump and a membrane module). In this case, the volume of the tank should be made as small as possible to avoid contact time with ozone.
【００３１】しかし、図２の実施形態は、循環槽または
膜供給槽にオゾンを直接注入した構成であるが、その場
合、循環槽または膜供給水槽への原水の導入について
は、一定流量で行われることが望ましい。従って、図３
に示すように、循環槽または膜供給槽の前に、バッファ
能力を持つ原水受槽１５を設けて、その原水受槽１５よ
り循環槽兼オゾン溶解槽１６の減少分を供給するように
するとよい。また、図４に示すように、循環槽兼オゾン
溶解槽１４の一部を仕切り、それぞれの仕切られた部分
に凝集剤の投入とオゾンのみを溶解させることができ
る。図３または図４の場合、オゾンの浴解方式は一般的
にディフューザ式とする。However, in the embodiment shown in FIG. 2, ozone is directly injected into the circulation tank or the membrane supply tank, but in that case, the raw water is introduced into the circulation tank or the membrane supply water tank at a constant flow rate. It is desirable to be seen. Therefore, FIG.
As shown in, a raw water receiving tank 15 having a buffering capacity may be provided in front of the circulation tank or the membrane supply tank, and the reduced amount of the circulation tank / ozone dissolving tank 16 may be supplied from the raw water receiving tank 15. Further, as shown in FIG. 4, it is possible to partition a part of the circulation tank / ozone dissolving tank 14 and to add the coagulant and dissolve only ozone into each partitioned portion. In the case of FIG. 3 or FIG. 4, the ozone bath dissolution method is generally a diffuser method.
【００３２】また、膜ろ過装置６の循環槽の容量は、配
管の容量も含めて５分以内で膜ろ過処理が可能な分のろ
過水量とすることが望ましい。そこで、図３の場合は、
循環槽兼オゾン溶解槽１６の容積を調整することで滞留
時間を５分以内とすることができる。図４の場合は、循
環槽兼オゾン溶解槽１４の仕切りの位置を変更すること
で滞留時間を変更することができる。なお、オゾン溶解
槽には、排オゾンガスが発生するため、排オゾンガスは
排オゾン設備に導入されて処理される。排オゾン設備の
形式は、活性炭式、燃焼式、触媒式等どの形式でも問題
がない。Further, it is desirable that the capacity of the circulation tank of the membrane filtration device 6, including the capacity of the pipes, be the amount of filtered water that can be subjected to the membrane filtration treatment within 5 minutes. Therefore, in the case of FIG.
By adjusting the volume of the circulation tank / ozone dissolving tank 16, the residence time can be kept within 5 minutes. In the case of FIG. 4, the residence time can be changed by changing the position of the partition of the circulation tank / ozone dissolving tank 14. Since exhaust ozone gas is generated in the ozone dissolving tank, the exhaust ozone gas is introduced into the exhaust ozone facility for processing. There is no problem with the type of exhaust ozone equipment such as activated carbon type, combustion type, catalytic type, etc.
【００３３】（２）本発明の膜ろ過装置について説明す
る。膜ろ過装置は、膜供給水にオゾンが溶解された状態
で膜ろ過することにより、常にオゾンによる前処理が行
われている状態で膜ろ過するために、膜の目詰まりを防
止することができる。かつ高い透過流束を得ることがで
きる。膜ろ過装置のろ過膜は、濁質成分および細菌類を
除去することができる膜であり、精密ろ過膜または限外
ろ過膜が用いられる。精密ろ過膜の場合は、孔径０．０
１〜０．４５μｍのものを用いられ、限外ろ過膜の場合
は、分画分子量１０００〜２０万ダルトンのものを用い
られる。そして、膜モジュールの形状は、中空糸状、ス
パイラル状、チューブラ状、平膜状溝が用いられる。(2) The membrane filtration device of the present invention will be described. The membrane filtration device can prevent clogging of the membrane by performing membrane filtration in a state where ozone is dissolved in the membrane feed water, and performing membrane filtration in the state where the pretreatment with ozone is always performed. . And a high permeation flux can be obtained. The filtration membrane of the membrane filtration device is a membrane capable of removing turbid components and bacteria, and a microfiltration membrane or an ultrafiltration membrane is used. In case of microfiltration membrane, pore size is 0.0
1 to 0.45 μm is used, and in the case of an ultrafiltration membrane, a molecular weight cutoff of 1,000 to 200,000 daltons is used. The shape of the membrane module is a hollow fiber shape, a spiral shape, a tubular shape, or a flat membrane shape groove.
【００３４】膜素材およびポッティング部は、高濃度の
オゾンに接触するために、耐オゾン性の素材を使うこと
が望ましい。膜素材については、フッ化ビニリデン重合
体樹脂等の耐オゾン性の有機樹脂またはセラミック等の
無機材料を用いることができる。また、膜ろ過への通水
方式は、全量ろ過方式とクロスフローろ過方式があり、
どちらの通水方式でも問題はない。Since the membrane material and the potting portion come into contact with high-concentration ozone, it is desirable to use an ozone-resistant material. As the film material, an ozone resistant organic resin such as a vinylidene fluoride polymer resin or an inorganic material such as a ceramic can be used. In addition, the water flow system for membrane filtration has a total volume filtration system and a cross flow filtration system,
There is no problem with either water flow system.
【００３５】クロスフローろ過方式の場合、図１または
図２の処理フローでは、循環槽３または循環槽兼オゾン
溶解槽１４に循環水を戻すのが一般的であるが、望まし
くは膜供給ポンプ５の直前に戻すことにより、さらにオ
ゾン消費量を削減することができる。図３および図４の
場合は、循環水の返送箇所が、原水受槽１５（図４の
場合は循環兼オゾン溶解槽１４のオゾンが溶解させてな
い部分）、循環槽兼オゾン溶解槽１６（図４の場合は
循環槽兼オゾン溶解槽１４のオゾンを溶解させている部
分）、膜供給ポンプ５の直前の３個所が考えられる
が、オゾンの消費量を削減するためには、の膜供給ポ
ンプ５の直前に返送する方式が最も望ましい。なお、膜
供給ポンプ５は、オゾンが溶解した水を送るため、耐オ
ゾン性のある素材で構成されたポンプを用いなければな
らない。In the case of the cross-flow filtration system, in the process flow of FIG. 1 or 2, it is common to return the circulating water to the circulating tank 3 or the circulating tank / ozone dissolving tank 14, but preferably the membrane supply pump 5 By returning to just before, it is possible to further reduce the ozone consumption. In the case of FIG. 3 and FIG. 4, the circulating water is returned to the raw water receiving tank 15 (in the case of FIG. 4, the portion of the circulation / ozone dissolution tank 14 where ozone is not dissolved), the circulation tank / ozone dissolution tank 16 (FIG. In the case of 4, there are three parts immediately before the membrane supply pump 5 in the circulation tank / ozone dissolution tank 14 where the ozone is dissolved. However, in order to reduce the consumption of ozone, the membrane supply pump The method of returning the item immediately before 5 is most desirable. Since the membrane supply pump 5 sends water in which ozone is dissolved, it is necessary to use a pump made of a material having ozone resistance.
【００３６】（３）本発明のオゾンの注入制御について
説明する。本実施形態では、膜ろ過水の残留オゾン濃度
をオゾン検出器１２で計測して、オゾン発生器２を操作
してオゾン注入量を制御する方法である。オゾン発生器
２で発生したオゾンは、オゾン溶解槽１０，１４，１６
とオゾン溶解槽兼接触槽１１に供給されるが、各供給配
管にバルブ（図示なし）を設けて、オゾン検出器１２で
計測された残留オゾン濃度に応じてバルブの開度を調整
することによって、調整することができる。または、オ
ゾン濃度の注入制御は、膜供給水のオゾン濃度を制御目
的値にすることも考えられるが、この場合、膜ろ過にお
ける短時間でも膜の表面の目詰まり物質とオゾンが反応
してオゾンが消費される場合があるため、膜ろ過水の残
留オゾン濃度を制御目的値とすることが望ましい。(3) The ozone injection control of the present invention will be described. In this embodiment, the residual ozone concentration of the membrane filtration water is measured by the ozone detector 12, and the ozone generator 2 is operated to control the ozone injection amount. The ozone generated by the ozone generator 2 is stored in the ozone dissolving tanks 10, 14, 16
And the ozone dissolution tank / contact tank 11 are provided. By providing a valve (not shown) in each supply pipe and adjusting the opening degree of the valve according to the residual ozone concentration measured by the ozone detector 12. , Can be adjusted. Alternatively, the ozone concentration injection control may be performed by setting the ozone concentration of the water supplied to the membrane to the control target value. In this case, the clogging substance on the membrane surface reacts with ozone even in a short time during membrane filtration. Since it may be consumed, it is desirable to use the residual ozone concentration of the membrane filtration water as the control target value.
【００３７】なお、オゾン溶解槽におけるオゾンの注入
率は、膜ろ過水の残留オゾン濃度によりフィードバック
されて決定される。なお、原水のオゾン要求量に変動が
ある場合は、膜ろ過水の残留オゾン濃度を溶存オゾン濃
度検出器で測定して、オゾン注入率のフィードバック制
御を行うこともできる。むろん、オゾン検出器１２は、
ＣＰＵ（中央処理装置）を用いて検出してもよい。The injection rate of ozone in the ozone dissolving tank is determined by feeding back the residual ozone concentration of the membrane filtration water. When the raw water ozone demand varies, the residual ozone concentration of the membrane-filtered water may be measured by a dissolved ozone concentration detector to perform feedback control of the ozone injection rate. Of course, the ozone detector 12
It may be detected using a CPU (central processing unit).
【００３８】（４）本発明のオゾン接触槽について説明
する。本発明では、膜ろ過装置の後段に、オゾン溶解槽
を兼ねるオゾン接触槽が設けられている。このような膜
ろ過装置の後段にオゾン溶解槽兼接触槽１１が設けられ
ており、膜ろ過水の残留オゾン濃度によって、オゾン溶
解槽兼接触槽１１へのオゾン注入率を調整することがで
き、有機物質とのオゾン処理を十分行うことが可能であ
る。この膜ろ過装置６の後段に設けたオゾン溶解槽兼接
触槽の目的は、有機物とのオゾン反応に必要な接触時
間を確保すること、オゾンを再注入して、オゾン反応
に必要なオゾンを補充することにある。そして、オゾン
接触槽の装置形式は、Ｕチューブ式、ディフューザ式、
インジェクタ式、下降注入式等のどの形式も可能であ
る。しかし、オゾンを注入した膜ろ過水に対して、オゾ
ンを溶解させており、高濃度のオゾンを溶解させること
は必要はない。装置形式は、接触時間を十分に確保する
ことができるディフューザ式が好ましい。オゾン接触槽
における接触時間は、有機物との十分な反応時間を確保
するために５分以上必要である。なお、オゾン接触槽に
おいても排オゾンガスが発生するため、排オゾンガスは
排オゾン設備に導入されて処理される。排オゾン設備の
形式は、活性炭式、燃焼式、触媒式等どの形式でも問題
がない。(4) The ozone contact tank of the present invention will be described. In the present invention, an ozone contact tank which doubles as an ozone dissolving tank is provided at the subsequent stage of the membrane filtration device. An ozone dissolving tank / contact tank 11 is provided at the subsequent stage of such a membrane filtering device, and the ozone injection rate into the ozone dissolving tank / contact tank 11 can be adjusted by the residual ozone concentration of the membrane filtration water. It is possible to sufficiently perform ozone treatment with an organic substance. The purpose of the ozone dissolution tank / contact tank provided in the latter stage of the membrane filtration device 6 is to secure the contact time necessary for the ozone reaction with the organic matter, re-inject the ozone, and replenish the ozone necessary for the ozone reaction. To do. And the device type of the ozone contact tank is U-tube type, diffuser type,
Any type such as an injector type and a downward injection type is possible. However, ozone is dissolved in the membrane-filtered water into which ozone is injected, and it is not necessary to dissolve high-concentration ozone. The device type is preferably a diffuser type capable of ensuring a sufficient contact time. The contact time in the ozone contact tank is required to be 5 minutes or more in order to secure a sufficient reaction time with an organic substance. Since exhausted ozone gas is also generated in the ozone contact tank, the exhausted ozone gas is introduced into the exhausted ozone equipment for processing. There is no problem with the type of exhaust ozone equipment such as activated carbon type, combustion type, catalytic type, etc.
【００３９】（５）本発明の活性炭処理装置について説
明する。活性炭処理装置８は、オゾンと反応して生物易
分解性になった有機物質を吸着除去すると共に、オゾン
反応で生成した副生成物を除くためのものであり、図６
の従来例で使用されるものと同様のものである。(5) The activated carbon treatment apparatus of the present invention will be described. The activated carbon treatment device 8 is for adsorbing and removing organic substances that have become easily biodegradable by reacting with ozone, and for removing by-products generated by the ozone reaction.
Is the same as that used in the conventional example.
【００４０】[0040]
【実施例】以下、本発明の実施例について説明する。こ
の実施例では、従来例を比較例とした比較実験と、実施
例の試験結果に基づいて説明する。なお、この実施例に
よって、本発明に限定を加えるものではない。EXAMPLES Examples of the present invention will be described below. This example will be described based on a comparative experiment using a conventional example as a comparative example and the test results of the example. The present invention is not limited to the embodiment.
【００４１】（実施例１）実施例１は、図１の処理フロ
ーによる水処理装置である。実施例１に対する比較例１
は、図６の処理フローによる水処理装置である。実施例
１と比較例１の実験装置および実験条件は、表１に示す
通りである。この比較実験におけるオゾン注入率の結果
は、表２に示した。表２に示したように、比較例１のオ
ゾン注入率が５ｍｇ／Ｌであったのに対して、実施例１
の場合は、前段オゾン注入率と後段オゾン注入率とを合
わせた総オゾン注入率が３ｍｇ／Ｌであり、実施例１で
は、オゾン消費量を従来例より低減することができた。(Example 1) Example 1 is a water treatment apparatus according to the treatment flow of FIG. Comparative Example 1 to Example 1
Is a water treatment device according to the treatment flow of FIG. The experimental apparatus and experimental conditions for Example 1 and Comparative Example 1 are as shown in Table 1. The results of the ozone injection rate in this comparative experiment are shown in Table 2. As shown in Table 2, while the ozone injection rate of Comparative Example 1 was 5 mg / L, Example 1
In this case, the total ozone injection rate, which is the sum of the front-stage ozone injection rate and the second-stage ozone injection rate, is 3 mg / L, and in Example 1, the ozone consumption amount could be reduced as compared with the conventional example.
【００４２】表３には、この比較実験による被処理水
（原水）とそれぞれの処理水質を示している。表３から
明らかなように、実施例の場合の活性炭処理水の臭素酸
イオン濃度は、５μｇ／ｍＬであり、比較例１の場合
は、２０μｇ／ｍＬであり、従来例より実施例がより良
好な水質を得ることができた。その他の水質項目につい
ては、実施例および比較例とも差はなかった。Table 3 shows the treated water (raw water) and the quality of each treated water in this comparative experiment. As is clear from Table 3, the bromate ion concentration of the activated carbon-treated water in the case of the example was 5 μg / mL, and in the case of the comparative example 1, it was 20 μg / mL, and the example was better than the conventional example. I was able to obtain excellent water quality. Regarding other water quality items, there was no difference between the example and the comparative example.
【００４３】（実施例２）実施例２は、図２の処理フロ
ーによる水処理装置を使用したものである。実施例２の
実験装置および実験条件は、滞留時間を除いて、表１と
同じである。オゾン注入後膜ろ過までの滞留時間と、膜
ろ過後活性炭塔までの滞留時間の条件は、表４に示す通
りである。実施例２では、膜ろ過水のオゾン濃度が、
０．２〜０．４ｍｇ／Ｌとなるように循環槽兼オゾン溶
解槽１４にオゾンを注入して、膜ろ過処理を行った。ま
た、循環槽兼オゾン溶解槽１４へのオゾンを注入は、活
性炭処理水の紫外線吸光度（波長２６０ｎｍ）がほぼ同
等の値となるように、膜ろ過後段におけるオゾン注入率
を決定した。この実験結果は、表５に示した。表５から
明らかなように、オゾン注入後膜ろ過までの滞留時間が
５分を越えると必要なオゾン注入量は大きくなった。(Embodiment 2) Embodiment 2 uses a water treatment apparatus according to the treatment flow of FIG. The experimental apparatus and experimental conditions of Example 2 are the same as in Table 1 except for the residence time. The conditions of the residence time after the ozone injection until the membrane filtration and the residence time after the membrane filtration up to the activated carbon tower are as shown in Table 4. In Example 2, the ozone concentration of the membrane filtration water was
Ozone was injected into the circulation tank / ozone dissolution tank 14 so as to have a concentration of 0.2 to 0.4 mg / L, and membrane filtration treatment was performed. Further, when ozone was injected into the circulation tank / ozone dissolution tank 14, the ozone injection rate after the membrane filtration was determined so that the ultraviolet absorbance (wavelength 260 nm) of the activated carbon-treated water was almost the same value. The results of this experiment are shown in Table 5. As is clear from Table 5, when the residence time after the ozone injection until the membrane filtration exceeds 5 minutes, the required ozone injection amount becomes large.
【００４４】（実施例３）実施例３は、図２の処理フロ
ーによる水処理装置を使用したものである。実施例３
は、オゾン注入後膜ろ過までの滞留時間を５分とし、循
環槽兼オゾン溶解槽１４におけるオゾン注入率は、２ｐ
ｐｍ、オゾン溶解槽兼接触槽１１におけるオゾン注入率
は、ｌｐｐｍとした。その他の実験装置および実験条件
は、表１と同じである。この実験では、膜ろ過装置６の
後段のオゾン溶解槽兼接触槽１１における滞留時間の変
化による影響について調査した。図５に示すように、オ
ゾン溶解槽兼接触槽１１における滞留時間を変化させ
て、膜ろ過後のオゾン溶解槽兼接触槽１１におけるオゾ
ン処理水の紫外線吸光度（波長２６０ｎｍ、５ｃｍセル
使用）の変化を示している。図５から明らかなように、
オゾン注入後膜ろ過までの滞留時間が５分の場合でも、
オゾン溶解槽兼接触槽１１における滞留時間は５分以上
が必要であった。(Embodiment 3) Embodiment 3 uses a water treatment apparatus according to the treatment flow of FIG. Example 3
Is 5 minutes after the ozone injection and before the membrane filtration, and the ozone injection rate in the circulation tank and ozone dissolution tank 14 is 2 p.
The ozone injection rate in the pm and ozone dissolution tank / contact tank 11 was set to 1 ppm. Other experimental apparatus and experimental conditions are the same as in Table 1. In this experiment, the influence of the change in the residence time in the ozone dissolution tank / contact tank 11 after the membrane filtration device 6 was investigated. As shown in FIG. 5, by changing the residence time in the ozone dissolution tank / contact tank 11, the ultraviolet absorbance (wavelength 260 nm, 5 cm cell used) of the ozone-treated water in the ozone dissolution tank / contact tank 11 after membrane filtration was changed. Is shown. As is clear from FIG.
Even if the residence time after the ozone injection until the membrane filtration is 5 minutes,
The residence time in the ozone dissolution tank / contact tank 11 required 5 minutes or more.
【００４５】[0045]
【表１】 [Table 1]
【００４６】[0046]
【表２】 [Table 2]
【００４７】[0047]
【表３】 [Table 3]
【００４８】[0048]
【表４】 [Table 4]
【００４９】[0049]
【表５】 [Table 5]
【００５０】[0050]
【発明の効果】上記のように、本発明の水処理装置及び
処理方法によれば、以下の効果を得ることができる。
（１）オゾン注入率を小さくすることができので、水処
理に要するオゾン消費を抑制することができる。
（２）オゾンの注入量を抑制することができるので、オ
ゾンによる副生成物の発生を低減することができる利点
があり、活性炭の寿命低下を抑制することができる利点
がある。
（３）原水の水質にオゾン溶解度が依存するので、膜ろ
過水中の残存オゾン濃度を計測して、オゾン溶解槽に注
入するオゾン注入量を調整することができるので、必要
以上に多量のオゾンを供給することなく、最適な量のオ
ゾンを注入することができるので、水処理装置のオゾン
酸化による影響を低減することができる利点がある。As described above, according to the water treatment apparatus and treatment method of the present invention, the following effects can be obtained. (1) Since the ozone injection rate can be reduced, ozone consumption required for water treatment can be suppressed. (2) Since the injection amount of ozone can be suppressed, there is an advantage that the generation of by-products due to ozone can be reduced, and a reduction in the life of activated carbon can be suppressed. (3) Since the ozone solubility depends on the water quality of the raw water, it is possible to measure the residual ozone concentration in the membrane filtration water and adjust the ozone injection amount to be injected into the ozone dissolution tank. Since the optimum amount of ozone can be injected without supplying it, there is an advantage that the influence of ozone oxidation of the water treatment device can be reduced.
【図１】本発明の一実施形態の処理フローを示す図であ
る。FIG. 1 is a diagram showing a processing flow of an embodiment of the present invention.
【図２】本発明の他の実施形態の処理フローを示す図で
ある。FIG. 2 is a diagram showing a processing flow of another embodiment of the present invention.
【図３】本発明の他の実施形態の処理フローを示す図で
ある。FIG. 3 is a diagram showing a processing flow of another embodiment of the present invention.
【図４】本発明の他の実施形態の処理フローを示す図で
ある。FIG. 4 is a diagram showing a processing flow of another embodiment of the present invention.
【図５】実施例３における紫外線吸光度のオゾン溶解槽
兼接触槽における経時変化を示したものである。FIG. 5 shows a change with time in ultraviolet absorbance of Example 3 in an ozone dissolving tank and a contact tank.
【図６】従来例の処理フローを示す図である。FIG. 6 is a diagram showing a processing flow of a conventional example.
【図７】従来例の処理フローを示す図である。FIG. 7 is a diagram showing a processing flow of a conventional example.
１ オゾン溶解槽兼接触槽 ２ オゾン発生器 ３ 循環槽または膜供給水槽 ４ 凝集剤注入ポンプ ５ 膜供給ポンプ ６ 膜ろ過装置 ７ 循環ライン ８ 活性炭処理装置（活性炭塔） ９ オゾン接触槽 １０ オゾン溶解槽 １１ オゾン溶解槽兼接触槽 １２ オゾン検出器 １３ 排オゾン処理設備 １４ 循環槽兼オゾン溶解槽 １５ 原水受槽 １６ 循環槽兼オゾン溶解槽 1 Ozone dissolution tank and contact tank 2 Ozone generator 3 Circulation tank or membrane supply water tank 4 Flocculant injection pump 5 membrane supply pump 6 Membrane filtration device 7 circulation line 8 Activated carbon processing equipment (activated carbon tower) 9 Ozone contact tank 10 ozone dissolution tank 11 Ozone dissolution tank and contact tank 12 Ozone detector 13 Waste ozone treatment equipment 14 Circulation tank and ozone dissolution tank 15 Raw water receiving tank 16 Circulation tank and ozone dissolution tank
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ Ｃ０２Ｆ 9/00 ５０４ Ｃ０２Ｆ 9/00 ５０４Ｂ ５０４Ｃ (72)発明者 土屋 博嗣 東京都千代田区丸の内一丁目１番２号 日本鋼管株式会社内 (72)発明者 峯岸 寅太郎 東京都千代田区丸の内一丁目１番２号 日本鋼管株式会社内 (72)発明者 水野 健一郎 東京都千代田区丸の内一丁目１番２号 日本鋼管株式会社内 (72)発明者 藤井 康二郎 東京都千代田区内幸町一丁目１番１号 旭化成工業株式会社内 (72)発明者 磯村 欽三 東京都港区虎ノ門一丁目１番３号 磯村 豊水機工株式会社内 (72)発明者 中谷 健治 東京都港区虎ノ門一丁目１番３号 磯村 豊水機工株式会社内 (72)発明者 本山 信行 東京都日野市富士町１番地 富士電機株 式会社内 (72)発明者 高橋 和孝 東京都日野市富士町１番地 富士電機株 式会社内 (72)発明者 山根 浩靖 東京都日野市富士町１番地 富士電機株 式会社内 (56)参考文献 特開 平11−277081（ＪＰ，Ａ) 特開 平11−239789（ＪＰ，Ａ) 特開 平10−309577（ＪＰ，Ａ) 特開 平10−113659（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) C02F 1/78 C02F 1/44 C02F 9/00 ─────────────────────────────────────────────────── ─── Continuation of the front page (51) Int.Cl. 7 Identification symbol FI C02F 9/00 504 C02F 9/00 504B 504C (72) Inventor Hirotsugu Tsuchiya 1-2-1, Marunouchi, Chiyoda-ku, Tokyo Nippon Steel Pipe stock In-company (72) Inventor Torataro Minegishi Marunouchi 1-2-2 Marunouchi, Chiyoda-ku, Tokyo Japan Steel Pipe Co., Ltd. (72) Inventor Kenichiro Mizuno 1-2-1 Marunouchi Chiyoda-ku, Tokyo Nippon Steel Pipe (72) ) Inventor Kojiro Fujii 1-1-1, Uchisaiwaicho, Chiyoda-ku, Tokyo Inside Asahi Kasei Co., Ltd. (72) Inventor Kinzo Isomura 1-3 1-3 Toranomon, Minato-ku, Tokyo Inside Isomura Hosui Kiki Co., Ltd. (72) Invention Kenji Nakatani 1-3-1 Toranomon, Minato-ku, Tokyo In Isomura Hosui Kiko Co., Ltd. (72) Inventor Nobuyuki Motoyama Hino, Tokyo Shishimachi No. 1 Fuji Electric Co., Ltd. (72) Inventor Kazutaka Takahashi No. 1 Fujimachi, Hino-shi, Tokyo Fuji Electric Co., Ltd. (72) Inventor Hiroyasu Yamane No. 1 Fuji-cho, Hino, Tokyo Fuji Electric Co., Ltd. In-house (56) Reference JP-A-11-270881 (JP, A) JP-A-11-239789 (JP, A) JP-A-10-309577 (JP, A) JP-A-10-113659 (JP, A) ) (58) Fields surveyed (Int.Cl. 7 , DB name) C02F 1/78 C02F 1/44 C02F 9/00
Claims (7)
て、 膜ろ過装置の前段に、オゾン溶解槽と前記オゾン溶解槽
にオゾンを注入するオゾン注入設備とを備え、前記膜ろ
過装置からの膜ろ過水中に残留する残留オゾン濃度が所
定範囲内となるように、前記残留オゾン濃度の測定値に
基づいて、前記オゾン溶解槽に供給されるオゾン注入量
を調整するとともに、前記膜ろ過装置の後段のオゾン溶
解槽兼接触槽にオゾンを注入し、膜ろ過水をオゾン接触
させて水処理することを特徴とする水処理方法。1. A water treatment method using ozone oxidation, comprising an ozone dissolving tank and an ozone injecting facility for injecting ozone into the ozone dissolving tank before the membrane filtering apparatus, and the membrane filtering from the membrane filtering apparatus. Based on the measured value of the residual ozone concentration, the ozone injection amount supplied to the ozone dissolution tank is adjusted so that the residual ozone concentration remaining in the water falls within a predetermined range, and at the latter stage of the membrane filtration device. A water treatment method comprising injecting ozone into an ozone dissolution tank and a contact tank and bringing the membrane-filtered water into contact with ozone for water treatment.
０ｍｇ／Ｌの範囲内となるように、前記オゾン注入量を
調整することを特徴とする請求項１に記載の水処理方
法。2. The residual ozone concentration is from 0.05 to 1.
The water treatment method according to claim 1, wherein the ozone injection amount is adjusted so as to be within a range of 0 mg / L.
装置の膜ろ過出口に設置したオゾン検出器により連続的
に膜ろ過水の残留オゾン濃度を測定し、前記膜ろ過水中
の残留オゾン濃度が、０．０５〜１．０ｍｇ／Ｌの範囲
内となるように、前記残留オゾン濃度の測定値に基づい
て、前記オゾン注入量をフィードバック制御し、前記残
留オゾン濃度を前記範囲内に調整することを特徴とする
請求項１に記載の水処理方法。3. The ozone injection amount is adjusted by continuously measuring the residual ozone concentration of the membrane filtration water by an ozone detector installed at the membrane filtration outlet of the membrane filtration device, and measuring the residual ozone concentration in the membrane filtration water. Is controlled within the range of 0.05 to 1.0 mg / L based on the measured value of the residual ozone concentration by feedback controlling the ozone injection amount and adjusting the residual ozone concentration within the range. The water treatment method according to claim 1, wherein
と前記オゾン溶解槽にオゾンを注入するオゾン注入設備
とを備え、前記オゾン溶解槽または前記オゾン注入設備
から前記膜ろ過装置までのオゾン滞留時間が５分以内で
あり、かつ前記オゾン溶解槽兼接触槽における滞留時間
が５分以上であることを特徴とする請求項１，２または
３に記載の水処理方法。4. An ozone dissolving tank and an ozone injecting equipment for injecting ozone into the ozone dissolving tank are provided in the preceding stage of the membrane filtering device, and ozone from the ozone dissolving tank or the ozone injecting equipment to the membrane filtering device. 4. The water treatment method according to claim 1, wherein the residence time is within 5 minutes, and the residence time in the ozone dissolution tank / contact tank is 5 minutes or more.
で膜ろ過し、そのろ過水をオゾン溶解槽兼接触槽に送っ
て水処理する水処理装置であって、 前記膜ろ過装置の前段に、オゾン溶解槽と前記オゾン溶
解槽にオゾンを注入するオゾン注入設備とを備え、 前記膜ろ過装置の膜ろ過出口に設置した膜ろ過水中の残
留オゾン濃度を計測するオゾン検出器と、 前記オゾン検出器によって膜ろ過水中の残留オゾン濃度
を測定し、その計測値に基づいて、前記オゾン溶解槽に
供給されるオゾン注入量を調整し、膜ろ過水中の残留オ
ゾン濃度を所定範囲内とするように制御する制御手段と
を具備することを特徴とする水処理装置。5. A water treatment device in which ozone is dissolved in water to be treated, membrane filtration is performed by a membrane filtration device, and the filtered water is sent to an ozone dissolution tank / contact tank to treat the water. In the first stage, an ozone dissolution tank and an ozone injection facility for injecting ozone into the ozone dissolution tank are provided, and an ozone detector for measuring the residual ozone concentration in the membrane filtration water installed at the membrane filtration outlet of the membrane filtration device, and The residual ozone concentration in the membrane filtered water is measured by an ozone detector, and the ozone injection amount supplied to the ozone dissolution tank is adjusted based on the measured value so that the residual ozone concentration in the membrane filtered water falls within a predetermined range. A water treatment device comprising:
供給槽を設け、前記循環槽または膜供給槽がオゾン溶解
槽を兼ねることを特徴とする請求項５に記載の水処理装
置。6. The water treatment apparatus according to claim 5, wherein a circulation tank or a membrane supply tank is provided in front of the membrane filtration device, and the circulation tank or the membrane supply tank also serves as an ozone dissolution tank.
る原水受水槽と循環槽または膜供給槽が設けられ、前記
原水受水槽に凝集剤を供給し、前記循環槽または膜供給
槽にオゾンを供給するようにしたことを特徴とする請求
項５または６に記載の水処理装置。7. A raw water receiving tank for receiving raw water and a circulation tank or a membrane supply tank are provided in front of the membrane filtration device, and a coagulant is supplied to the raw water receiving tank to provide the circulation tank or the membrane supply tank. The water treatment device according to claim 5, wherein ozone is supplied to the water treatment device.
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|---|---|---|---|
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|---|---|---|---|
| JP28270498A JP3449247B2 (en) | 1998-10-05 | 1998-10-05 | Water treatment method and apparatus |
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