JPH11277060A - Apparatus for treating water containing manganese - Google Patents
Apparatus for treating water containing manganeseInfo
- Publication number
- JPH11277060A JPH11277060A JP10083988A JP8398898A JPH11277060A JP H11277060 A JPH11277060 A JP H11277060A JP 10083988 A JP10083988 A JP 10083988A JP 8398898 A JP8398898 A JP 8398898A JP H11277060 A JPH11277060 A JP H11277060A
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- Japan
- Prior art keywords
- ozone
- water
- membrane
- manganese
- backwash
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、マンガン含有水
を、オゾン処理装置、膜濾過装置及び活性炭吸着装置に
順次通水して処理するマンガン含有水処理装置に係り、
特に、オゾン処理水を膜濾過する膜濾過装置を効果的に
逆洗して濾過効率を高く維持するように改良されたマン
ガン含有水処理装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a manganese-containing water treatment apparatus for treating manganese-containing water by sequentially passing it through an ozone treatment apparatus, a membrane filtration apparatus and an activated carbon adsorption apparatus.
In particular, the present invention relates to a manganese-containing water treatment apparatus improved so as to effectively backwash a membrane filtration apparatus for membrane-filtering ozonized water to maintain high filtration efficiency.
【０００２】[0002]
【従来の技術及び先行技術】マンガンを含有する原水の
処理方法としては、溶解性マンガンを塩素等を用いて酸
化することにより不溶性の沈殿として除去する方法が一
般に採用されてきたが（特開平９−５７２６３号公
報）、この方法において、例えば膜濾過装置でマンガン
の不溶物を除去する場合、原水中に有機成分が共存する
と、膜面に有機成分のケーク層又はゲル層が生成して膜
の透過流束が低減する。このため、原水中の有機成分は
予め除去する必要がある。また、例えば原水中にフミン
酸が存在すると、酸化剤として添加した塩素とフミン酸
とが反応してトリハロメタンが生成するおそれがあるた
め、この点からも有機成分の除去が必要となる。2. Description of the Related Art As a method of treating raw water containing manganese, a method of removing soluble manganese as insoluble precipitates by oxidizing it with chlorine or the like has been generally employed (Japanese Patent Laid-Open No. Hei 9 (1994) -108). In this method, when an insoluble matter of manganese is removed by, for example, a membrane filtration device, when an organic component coexists in raw water, a cake layer or a gel layer of the organic component is formed on the membrane surface to form a membrane. The permeation flux is reduced. Therefore, it is necessary to remove the organic components in the raw water in advance. Further, for example, if humic acid is present in raw water, the chlorine added as an oxidizing agent may react with humic acid to generate trihalomethane. Therefore, it is necessary to remove organic components from this point as well.
【０００３】一方、有機成分の除去方法としては、凝集
沈殿・砂濾過による方法や、最近ではオゾン・活性炭処
理と膜濾過処理を組み合せた方法が採用されるようにな
っている（特開平６−３２８０６９号公報、特開平８−
８９９５９号公報）。On the other hand, as a method for removing organic components, a method using coagulation sedimentation and sand filtration, and a method combining ozone / activated carbon treatment and membrane filtration treatment have recently been adopted (Japanese Patent Application Laid-Open No. Hei 6-1994). No. 328069, JP-A-8-
No. 89959).
【０００４】また、本発明者らは、膜濾過装置の前段に
オゾン処理装置を配置することにより、膜濾過のファウ
リングを抑制して、高効率な運転が可能となることを見
出し、フミン等の有機物とマンガンが共存する系におけ
るオゾン・膜濾過処理法を提案している（特願平９−２
０９０６９号）。この方法において、特にオゾン耐性の
ある膜素材を用いた場合には、オゾン処理装置の流出水
中に残留オゾンが検出される条件で膜濾過を行うことが
可能であり、この場合には、膜面に析出する有機物や付
着生長する微生物スライム等による有機性の膜ファウリ
ングの原因物質となる成分を、その残存オゾンにより分
解ないし改質することにより、安定した膜濾過を継続す
ることができる。Further, the present inventors have found that by arranging an ozone treatment device in front of a membrane filtration device, fouling of membrane filtration can be suppressed and high-efficiency operation can be performed. Of ozone / membrane filtration in a system in which organic matter and manganese coexist (Japanese Patent Application No. 9-2).
No. 09069). In this method, in particular, when a membrane material having ozone resistance is used, membrane filtration can be performed under the condition that residual ozone is detected in the effluent of the ozone treatment apparatus. Stable membrane filtration can be continued by decomposing or reforming a component which causes organic membrane fouling due to organic substances precipitated on the surface of the membrane or microbial slime that adheres and grows with the remaining ozone.
【０００５】なお、このような膜濾過装置において、比
較的短期間で膜の目詰りが発生した場合には、膜濾過水
を逆洗水槽に貯留し、この逆洗水槽から膜の透過水側に
膜濾過水を逆流させる逆洗を定期的に行うことにより、
膜で阻止され膜面に付着した無機物質を系外へ押し出
し、効率的な膜濾過運転を継続できることが知られてい
る。[0005] In such a membrane filtration apparatus, when clogging of the membrane occurs in a relatively short period of time, the membrane filtered water is stored in a backwash water tank and the permeate water side of the membrane is removed from the backwash water tank. By periodically performing backwashing to reverse the membrane filtration water,
It is known that an inorganic substance that is blocked by a membrane and adheres to the membrane surface is pushed out of the system, and an efficient membrane filtration operation can be continued.
【０００６】[0006]
【発明が解決しようとする課題】ところで、オゾン処理
においては、オゾンは原水中のマンガンの酸化に優先的
に消費されるため、フミン等の有機物の酸化等のために
過剰のオゾンを用いると、オゾンによる酸化で生成した
不溶性の二酸化マンガンが更に酸化されて過マンガン酸
イオンとなって溶解し、これが膜を透過して膜濾過水の
水質を低下させることとなる。By the way, in the ozone treatment, ozone is preferentially consumed for oxidizing manganese in raw water. Therefore, if excessive ozone is used to oxidize organic substances such as humin, Insoluble manganese dioxide generated by oxidation with ozone is further oxidized and dissolved as permanganate ions, which permeate the membrane and lower the quality of the membrane filtered water.
【０００７】前述の如く、オゾン処理装置の流出水中に
残留オゾンが検出される条件でオゾン処理した水を膜濾
過する場合、原水中のマンガンが比較的低濃度であれ
ば、過マンガン酸イオンが殆ど生成しない条件でオゾン
を注入し、更にオゾンを残存させることも容易であるた
め、膜濾過水の水質低下の問題は殆どない。As described above, when membrane water is subjected to membrane filtration of ozone-treated water under the condition that residual ozone is detected in the effluent of the ozone treatment apparatus, if the concentration of manganese in the raw water is relatively low, the permanganate ion is reduced. Since it is easy to inject ozone under conditions that hardly generate ozone and further to allow ozone to remain, there is almost no problem of deterioration in water quality of the membrane filtered water.
【０００８】しかしながら、原水中のマンガンが高濃度
である場合には、オゾン処理水中にオゾンを残存させる
ためには、相当量のオゾンを注入する必要があり、この
結果、マンガンの酸化が進行して過マンガン酸イオンが
生成し、これが膜を透過する。However, when the concentration of manganese in raw water is high, it is necessary to inject a considerable amount of ozone in order to leave ozone in the ozonized water, and as a result, oxidation of manganese proceeds. To form permanganate ions, which permeate the membrane.
【０００９】膜を透過した過マンガン酸イオンは、逆洗
水槽で貯留されている間に残留オゾンが消失すると、二
酸化マンガンに還元され、不溶物として析出する。When the residual ozone disappears while the permanganate ions permeate the membrane while being stored in the backwash tank, they are reduced to manganese dioxide and precipitated as insolubles.
【００１０】このように二酸化マンガンが析出した逆洗
水槽内の貯留水を逆洗水として逆洗に用いると、膜の透
過水側に二酸化マンガンが付着し、ファウリングの原因
となる。[0010] If the water stored in the backwash water tank on which manganese dioxide is precipitated is used for backwash as backwash water, manganese dioxide adheres to the permeated water side of the membrane and causes fouling.
【００１１】本発明は上記従来の問題点を解決し、マン
ガン含有水を、オゾン処理装置（好ましくは、処理水中
にオゾンが残留するようなオゾン過剰の処理条件でオゾ
ン処理するオゾン処理装置）、膜濾過装置及び活性炭吸
着装置に順次通水して処理するマンガン含有水処理装置
において、オゾン処理水を膜濾過する膜濾過装置を効果
的に逆洗して濾過効率を高く維持することができるマン
ガン含有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 and provides an ozone treatment apparatus (preferably an ozone treatment apparatus for treating ozone under an ozone-excess treatment condition such that ozone remains in treated water). In a manganese-containing water treatment apparatus for treating water by sequentially passing water through a membrane filtration apparatus and an activated carbon adsorption apparatus, manganese capable of effectively backwashing a membrane filtration apparatus for membrane-filtering ozonized water to maintain high filtration efficiency. An object of the present invention is to provide a contained water treatment device.
【００１２】[0012]
【課題を解決するための手段】本発明のマンガン含有水
処理装置は、マンガン含有水を、オゾン処理装置、膜濾
過装置及び活性炭吸着装置に順次通水して処理するマン
ガン含有水処理装置において、該活性炭吸着装置からの
流出水を貯留する逆洗水槽と、該逆洗水槽と前記膜濾過
装置の透過水側とを連結する逆洗配管とを設けたことを
特徴とする。The manganese-containing water treatment apparatus according to the present invention is a manganese-containing water treatment apparatus for treating manganese-containing water by sequentially passing water through an ozone treatment apparatus, a membrane filtration apparatus, and an activated carbon adsorption apparatus. A backwash water tank for storing the effluent from the activated carbon adsorption device, and a backwash pipe connecting the backwash water tank and the permeated water side of the membrane filtration device are provided.
【００１３】本発明のマンガン含有水処理装置では、膜
濾過装置の膜濾過水中に膜を透過した過マンガン酸イオ
ンが含有されている場合でも、活性炭吸着装置におい
て、この過マンガン酸イオンを二酸化マンガンに還元し
て捕捉するため、活性炭吸着装置からの過マンガン酸イ
オン及び二酸化マンガンの流出は防止される。従って、
マンガンを殆ど含まない清浄な活性炭吸着装置の流出水
を逆洗水として用いることにより、効果的な逆洗を行え
る。[0013] In the manganese-containing water treatment apparatus of the present invention, even if permanganate ions permeated through the membrane are contained in the membrane filtration water of the membrane filtration apparatus, the permanganate ions are converted into manganese dioxide in the activated carbon adsorption apparatus. Thus, the outflow of permanganate ions and manganese dioxide from the activated carbon adsorption device is prevented. Therefore,
Effective backwashing can be performed by using the effluent of a clean activated carbon adsorption device containing almost no manganese as backwash water.
【００１４】[0014]
【発明の実施の形態】以下に図面を参照して本発明の実
施の形態を説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００１５】図１は本発明のマンガン含有水処理装置の
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 manganese-containing water treatment apparatus according to the present invention.
【００１６】図１のマンガン含有水処理装置において
は、原水をまず、原水槽１よりポンプＰ1によりオゾン
接触塔２に導入し、オゾン供給装置（図示略）からのオ
ゾン含有ガスを原水中に吹き込んでオゾン酸化処理し、
有機成分を酸化分解すると共に、マンガンを二酸化マン
ガンに酸化して不溶化する。このように有機成分の酸化
分解とマンガンの酸化を行うためには、このオゾン酸化
は、オゾン処理水中にオゾンが残存するようなオゾン過
剰の処理条件で行うことが好ましく、これにより、原水
中の有機成分を確実に酸化分解して膜の原水側の汚染を
防止して安定した膜濾過を継続することができる。この
ようなオゾン過剰の処理を行うには、オゾン接触塔２の
流出水中のオゾン濃度をセンサで検知し、このオゾン濃
度が所定範囲となるようにオゾン供給装置を制御する制
御器を設けるのが好ましい。また、原水中の有機成分濃
度を予め求めておくか又はセンサで検出し、この有機成
分濃度に応じてオゾン供給装置を制御する制御器を設け
ても良い。In the manganese-containing water treatment apparatus shown in FIG. 1, raw water is first introduced from a raw water tank 1 into an ozone contact tower 2 by a pump P1, and an ozone-containing gas from an ozone supply device (not shown) is introduced into the raw water. Ozone oxidation treatment
Organic components are oxidatively decomposed and manganese is oxidized to manganese dioxide to make it insoluble. In order to perform the oxidative decomposition of organic components and the oxidation of manganese in this manner, the ozone oxidation is preferably performed under ozone-excess treatment conditions such that ozone remains in the ozone-treated water. Organic components can be reliably oxidized and decomposed to prevent contamination on the raw water side of the membrane, and stable membrane filtration can be continued. In order to perform such an excess ozone treatment, a controller that detects the ozone concentration in the effluent of the ozone contact tower 2 with a sensor and controls the ozone supply device so that the ozone concentration is within a predetermined range is provided. preferable. Further, a controller may be provided that determines the concentration of the organic component in the raw water in advance or detects the concentration with a sensor, and controls the ozone supply device according to the concentration of the organic component.
【００１７】この場合、オゾン処理水中の残留オゾン濃
度が少な過ぎると有機成分の酸化分解が十分に進行せ
ず、逆に多過ぎると、マンガンの過酸化で過マンガン酸
イオンが多量に生成し、膜濾過装置で分離し得なくな
る。この過マンガン酸イオンは、後段の活性炭吸着塔４
で除去することができ、また、本発明では、活性炭吸着
塔４の流出水を膜濾過装置の逆洗水とすることから、残
留オゾンによる過マンガン酸イオンの生成は、処理水質
や膜の逆洗効果の面で大きな問題となることはないが、
過度に過剰のオゾンを注入することは、オゾン使用量の
増大、活性炭吸着塔の負荷の増大を招き、好ましくな
い。従って、このオゾン処理水中の残留オゾン濃度は、
０．２〜０．５ｍｇ／Ｌ程度となるような条件でオゾン
処理を行うのが好ましい。In this case, if the residual ozone concentration in the ozonized water is too low, the oxidative decomposition of the organic component does not sufficiently proceed. On the contrary, if the residual ozone concentration is too high, a large amount of permanganate ion is generated by manganese peroxidation, It cannot be separated by a membrane filtration device. This permanganate ion is supplied to the activated carbon adsorption tower 4 in the subsequent stage.
In the present invention, since the effluent of the activated carbon adsorption tower 4 is used as backwashing water of the membrane filtration device, the production of permanganate ions due to residual ozone is caused by the treatment water quality and the reverse of the membrane. There is no big problem in terms of washing effect,
Injecting an excessively large amount of ozone is not preferable because it causes an increase in the amount of used ozone and an increase in the load on the activated carbon adsorption tower. Therefore, the residual ozone concentration in this ozonated water is
It is preferable to perform the ozone treatment under the condition that the concentration is about 0.2 to 0.5 mg / L.
【００１８】なお、このような残留オゾン濃度となるよ
うなオゾン注入率は、原水の水質によっても異なるが、
通常の地下水、湧水等の処理においては、１〜３ｍｇ／
Ｌ程度である。Although the ozone injection rate at which such a residual ozone concentration is obtained varies depending on the quality of raw water,
In ordinary treatment of groundwater, spring water, etc., 1-3 mg /
It is about L.
【００１９】オゾン接触塔２では、上記オゾン注入率に
て、滞留時間１０〜１５分程度で処理するのが好まし
い。The ozone contact tower 2 is preferably treated at the above-mentioned ozone injection rate for a residence time of about 10 to 15 minutes.
【００２０】オゾン処理水は、次いで、ポンプＰ2によ
り、膜濾過装置３へ送給し、不溶物を固液分離する。Next, the ozonated water is fed to the membrane filtration device 3 by the pump P 2 to separate solid and liquid insolubles.
【００２１】この膜濾過装置３の膜種としては、精密濾
過（ＭＦ）膜、限外濾過（ＵＦ）膜等を用いることがで
き、濃縮水の循環系路を有するクロスフロー方式のもの
が好適である。As a membrane type of the membrane filtration device 3, a microfiltration (MF) membrane, an ultrafiltration (UF) membrane, or the like can be used, and a cross-flow type having a concentrated water circulation system is preferable. It is.
【００２２】この膜濾過装置３には、残留オゾンを含む
オゾン処理水が流入するため、膜濾過装置３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、４
フッ化ポリエチレンや２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 ozone-treated water containing residual ozone flows into the membrane filtration device 3, the membrane of the membrane filtration device 3 may be made of an inorganic material such as glass, alumina ceramic material, or metal material. For films and organic films, 4
It is preferable to use a fluorine-based material such as polyethylene fluoride or polyvinylidene difluoride, or a material having strong ozone corrosion resistance such as polyetheretherketone.
【００２３】膜濾過装置３の膜濾過水はポンプＰ3によ
り活性炭吸着塔４に送給される。この活性炭吸着塔４で
は、膜濾過水中に残留するオゾンが吸着除去されると共
に、マンガンの過酸化で生成した過マンガン酸イオンが
還元され、生成した二酸化マンガンが捕捉される。この
二酸化マンガンの捕捉を効率的に行うために、活性炭吸
着塔４の型式は、粒状活性炭を充填した固定床型が好ま
しい。なお、固定床型であれば上向流方式でも下向流方
式でも良いが、流動化の恐れがなく捕捉効率に優れるこ
とから、下向流方式が好適である。The membrane filtering device 3 of the membrane filtration water is fed to the activated carbon adsorption tower 4 by a pump P 3. In the activated carbon adsorption tower 4, ozone remaining in the membrane filtration water is adsorbed and removed, and permanganate ions generated by manganese peroxidation are reduced, and the generated manganese dioxide is captured. In order to efficiently capture the manganese dioxide, the type of the activated carbon adsorption tower 4 is preferably a fixed bed type packed with granular activated carbon. In addition, if it is a fixed bed type, an upward flow method or a downward flow method may be used, but a downward flow method is preferable because there is no fear of fluidization and the trapping efficiency is excellent.
【００２４】なお、流動床型の活性炭吸着塔を採用する
場合には、活性炭吸着塔の後段に砂濾過装置、膜濾過装
置等の固液分離装置を設けることにより、処理水への二
酸化マンガンの流出は防止されるが、この場合には装置
数が増えるため、固定床型の活性炭吸着塔を採用するの
が好ましい。When a fluidized bed type activated carbon adsorption tower is employed, a solid-liquid separation device such as a sand filtration device or a membrane filtration device may be provided at the subsequent stage of the activated carbon adsorption tower, so that manganese dioxide can be added to the treated water. Although outflow is prevented, in this case, the number of apparatuses increases, so it is preferable to employ a fixed bed type activated carbon adsorption tower.
【００２５】活性炭吸着塔４の流出水は二酸化マンガ
ン、その他の濁質や残留オゾンが除去された清澄度の高
い水であり、処理水槽（逆洗水槽）５に貯留され、適宜
系外へ排出される。The effluent from the activated carbon adsorption tower 4 is high-clarity water from which manganese dioxide, other turbidity and residual ozone have been removed, and is stored in a treated water tank (backwash water tank) 5 and discharged out of the system as appropriate. Is done.
【００２６】図示の装置では、処理水槽５の水をポンプ
Ｐ4を備える逆洗配管６より膜濾過装置３の膜の透過水
側に逆流させて逆洗を行う。[0026] In the illustrated apparatus, performs backwash by reverse flow of water treatment water tank 5 to the permeate side of the backwash pipe 6 from the membrane filtration unit 3 of the film with a pump P 4.
【００２７】この逆洗に用いる活性炭吸着塔４の流出水
は、前述の如く、二酸化マンガン等を含まない清浄度の
高い水であるため、膜の透過水側を汚染させることな
く、膜の原水側の膜面に付着した無機物質を効果的に押
し出し、系外へ排出することができる。As described above, the effluent from the activated carbon adsorption tower 4 used for the backwashing is high-purity water that does not contain manganese dioxide or the like. The inorganic substance attached to the film surface on the side can be effectively extruded and discharged out of the system.
【００２８】逆洗による押出水は、配管７より排出され
る。Extrusion water from the backwash is discharged from the pipe 7.
【００２９】この逆洗頻度等の逆洗条件には特に制限は
ないが、通常の場合、２０〜３０分程度の濾過運転毎に
０．５〜２分程度の逆洗を行い、逆洗水を２０〜５０Ｌ
／ｍｉｎで逆流させる。There are no particular restrictions on the backwashing conditions such as the frequency of backwashing, but in the usual case, backwashing is performed for about 0.5 to 2 minutes for each filtration operation of about 20 to 30 minutes, 20-50L
/ Min.
【００３０】[0030]
【実施例】以下に実施例及び比較例を挙げて本発明をよ
り具体的に説明する。The present invention will be described more specifically below with reference to examples and comparative examples.
【００３１】実施例１ 水道水に懸濁物質としてベントナイト、フミン酸ナトリ
ウム、硫酸マンガンをそれぞれ１０ｍｇ／Ｌ、２．５ｍ
ｇ／Ｌ、１ｍｇ−Ｍｎ／Ｌとなるように溶解した水を原
水として、図１に示す方法で処理した。Example 1 Bentonite, sodium humate and manganese sulfate were suspended in tap water at a concentration of 10 mg / L and 2.5 m, respectively.
Water treated as g / L and 1 mg-Mn / L was treated as raw water by the method shown in FIG.
【００３２】原水は６．５ｍ3／ｄａｙで処理し、オゾ
ン接触塔１では、オゾン注入率１．２ｍｇ−Ｏ3／Ｌ、
滞留時間１４分でオゾン接触塔１の流出水の残留オゾン
濃度を０．３〜０．３５ｍｇ−Ｏ3／Ｌに制御した。Raw water is treated at 6.5 m 3 / day, and the ozone contact tower 1 has an ozone injection rate of 1.2 mg-O 3 / L,
Controlled residual ozone concentration in the effluent of the ozone contact column 1 to 0.3~0.35mg-O 3 / L a residence time 14 minutes.
【００３３】膜濾過装置３としては、耐オゾン性の四フ
ッ化エチレン（ＰＴＦＥ、公称孔径０．２μｍ）平膜か
らなるスパイラル形状のＵＦ膜濾過モジュールを用い、
膜の濾過流束を２ｍ3／ｍ2／ｄａｙとして処理を行っ
た。この膜濾過装置３の膜濾過水は次いで活性炭吸着塔
４に約２５０Ｌ／Ｈｒ（６ｍ3／ｄａｙ）で通水した。
この活性炭吸着塔４としては粒状活性炭を充填した下向
流固定床式のものを用いた。As the membrane filtration device 3, a spiral UF membrane filtration module made of an ozone-resistant ethylene tetrafluoride (PTFE, nominal pore diameter 0.2 μm) flat membrane is used.
The treatment was performed at a filtration flux of 2 m 3 / m 2 / day. The membrane filtered water from the membrane filtration device 3 was then passed through the activated carbon adsorption tower 4 at about 250 L / Hr (6 m 3 / day).
As the activated carbon adsorption tower 4, a downflow fixed bed type packed with granular activated carbon was used.
【００３４】このときの膜濾過水及び処理水（活性炭吸
着塔４の流出水）の水質は表１に示す通りである。The water quality of the membrane filtered water and treated water (outflow water of the activated carbon adsorption tower 4) at this time is as shown in Table 1.
【００３５】[0035]
【表１】 [Table 1]
【００３６】このような装置において、処理水（活性炭
の吸着塔４の流出水）を逆洗水として、２０分に１回の
頻度で０．５分間、３０Ｌ／ｍｉｎで逆流させることに
より逆洗を行った。In such an apparatus, the treated water (the effluent from the activated carbon adsorption tower 4) is used as backwashing water, which is backwashed once every 20 minutes for 0.5 minute at 30 L / min. Was done.
【００３７】このような処理を３０日間継続した後の膜
の透過流束を調べ、結果を表２に示した。After such a treatment was continued for 30 days, the permeation flux of the membrane was examined, and the results are shown in Table 2.
【００３８】比較例１ 実施例１において、膜濾過装置の逆洗を、膜濾過水を用
いて行ったこと以外は全く同様にして処理を継続し、３
０日後の膜の透過流束を調べ、結果を表２に示した。Comparative Example 1 The procedure of Example 1 was repeated, except that the backwashing of the membrane filtration device was carried out using membrane filtered water.
After 0 day, the permeation flux of the membrane was examined, and the results are shown in Table 2.
【００３９】[0039]
【表２】 [Table 2]
【００４０】以上の結果より、活性炭吸着塔の流出水で
逆洗を行う本発明のマンガン含有水処理装置によれば、
膜を効果的に逆洗して、長期に亘り安定な運転を行える
ことがわかる。From the above results, according to the manganese-containing water treatment apparatus of the present invention for backwashing with the effluent of the activated carbon adsorption tower,
It can be seen that the membrane can be effectively backwashed and stable operation can be performed for a long period of time.
【００４１】[0041]
【発明の効果】以上詳述した通り、本発明のマンガン含
有水処理装置によれば、マンガン含有水を、オゾン処理
装置、膜濾過装置及び活性炭吸着装置に順次通水して処
理するマンガン含有水処理装置において、オゾン処理水
を膜濾過する膜濾過装置を効果的に逆洗して濾過効率を
高く維持することができる。As described in detail above, according to the manganese-containing water treatment apparatus of the present invention, manganese-containing water is treated by sequentially passing manganese-containing water through an ozone treatment apparatus, a membrane filtration apparatus and an activated carbon adsorption apparatus. In the treatment apparatus, a membrane filtration apparatus for membrane-filtering ozonized water can be effectively backwashed to maintain a high filtration efficiency.
【図１】本発明のマンガン含有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 manganese-containing water treatment apparatus of the present invention.
１ 原水槽 ２ オゾン接触塔 ３ 膜濾過装置 ４ 活性炭吸着塔 ５ 処理水槽 ６ 逆洗配管 1 Raw water tank 2 Ozone contact tower 3 Membrane filtration device 4 Activated carbon adsorption tower 5 Treatment water tank 6 Backwash pipe
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｃ０２Ｆ 9/00 ５０２ Ｃ０２Ｆ 9/00 ５０２Ｅ ５０２Ｈ ５０２Ｒ ５０３ ５０３Ａ ５０４ ５０４Ｂ ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 6 Identification code FI C02F 9/00 502 C02F 9/00 502E 502H 502R 503 503A 504 504B
Claims (2)
濾過装置及び活性炭吸着装置に順次に通水して処理する
マンガン含有水処理装置において、該活性炭吸着装置か
らの流出水を貯留する逆洗水槽と、該逆洗水槽と前記膜
濾過装置の透過水側とを連結する逆洗配管とを設けたこ
とを特徴とするマンガン含有水処理装置。In a manganese-containing water treatment apparatus for treating manganese-containing water by sequentially passing water through an ozone treatment apparatus, a membrane filtration apparatus, and an activated carbon adsorption apparatus, a backwash for storing effluent from the activated carbon adsorption apparatus. A manganese-containing water treatment apparatus, comprising: a water tank; and a backwash pipe connecting the backwash water tank and a permeated water side of the membrane filtration device.
は、該オゾン処理装置からの流出水中に所定量のオゾン
が残留するようにオゾンをマンガン含有水に対し添加す
るものであることを特徴とするマンガン含有水処理装
置。2. The ozone treatment apparatus according to claim 1, wherein the ozone is added to the manganese-containing water such that a predetermined amount of ozone remains in the effluent from the ozone treatment apparatus. Manganese-containing water treatment equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP08398898A JP3896687B2 (en) | 1998-03-30 | 1998-03-30 | Manganese-containing water treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP08398898A JP3896687B2 (en) | 1998-03-30 | 1998-03-30 | Manganese-containing water treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH11277060A true JPH11277060A (en) | 1999-10-12 |
| JP3896687B2 JP3896687B2 (en) | 2007-03-22 |
Family
ID=13817930
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP08398898A Expired - Fee Related JP3896687B2 (en) | 1998-03-30 | 1998-03-30 | Manganese-containing water treatment equipment |
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| Country | Link |
|---|---|
| JP (1) | JP3896687B2 (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| BE1014267A3 (en) * | 2001-06-27 | 2003-07-01 | Aqua Reverse Osmosis Systems A | Removal of iron from water by oxidation, comprises contacting water with ozone |
| KR100460385B1 (en) * | 2001-02-12 | 2004-12-14 | 최영규 | Method and apparatus for processing of ozone water treatment |
| KR100737352B1 (en) | 2006-12-27 | 2007-07-09 | 케미코아 주식회사 | Apparatus and method for reusing discharge water of a public bath |
| JP2016215140A (en) * | 2015-05-21 | 2016-12-22 | 株式会社川本製作所 | Filter device and control method of filter device |
| AT516359B1 (en) * | 2014-10-01 | 2021-06-15 | Deltacore Gmbh | Device for the filtration of water with a filter arrangement |
-
1998
- 1998-03-30 JP JP08398898A patent/JP3896687B2/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100460385B1 (en) * | 2001-02-12 | 2004-12-14 | 최영규 | Method and apparatus for processing of ozone water treatment |
| BE1014267A3 (en) * | 2001-06-27 | 2003-07-01 | Aqua Reverse Osmosis Systems A | Removal of iron from water by oxidation, comprises contacting water with ozone |
| KR100737352B1 (en) | 2006-12-27 | 2007-07-09 | 케미코아 주식회사 | Apparatus and method for reusing discharge water of a public bath |
| AT516359B1 (en) * | 2014-10-01 | 2021-06-15 | Deltacore Gmbh | Device for the filtration of water with a filter arrangement |
| JP2016215140A (en) * | 2015-05-21 | 2016-12-22 | 株式会社川本製作所 | Filter device and control method of filter device |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3896687B2 (en) | 2007-03-22 |
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