JP2002035554A - Method for treating water and its apparatus - Google Patents
Method for treating water and its apparatusInfo
- Publication number
- JP2002035554A JP2002035554A JP2000222786A JP2000222786A JP2002035554A JP 2002035554 A JP2002035554 A JP 2002035554A JP 2000222786 A JP2000222786 A JP 2000222786A JP 2000222786 A JP2000222786 A JP 2000222786A JP 2002035554 A JP2002035554 A JP 2002035554A
- Authority
- JP
- Japan
- Prior art keywords
- water
- membrane
- ozone
- raw water
- turbidity
- 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.)
- Pending
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Biological Treatment Of Waste Water (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
Abstract
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に係り、特に、膜
ろ過処理を用いた水処理方法および水処理装置に関す
る。TECHNICAL FIELD The present invention relates to a water supply system, a sewer system,
The present invention relates to a water treatment method for industrial water or wastewater treatment, and more particularly, to a water treatment method and a water treatment apparatus using a membrane filtration treatment.
【０００２】[0002]
【従来の技術】近年、浄水処理において、小規模水道を
中心に従来の凝集沈殿−砂ろ過処理の代替として、維持
管理性および省スペース化に優れた膜ろ過処理を用いる
ケースが増大しつつある。しかしながら、膜ろ過処理を
用いて水処理を行なった場合には、運転を継続すると、
膜供給水として膜ろ過処理に導入される原水中の懸濁物
質および有機物質等に起因して次のような現象が生じ
る。すなわち、膜面あるいは細孔内が経時的に汚れて膜
ろ過水量が低下し、あるいは膜間差圧が上昇する。2. Description of the Related Art In recent years, in water purification treatment, a membrane filtration treatment which is excellent in maintenance and space saving and space saving is increasing as an alternative to the conventional coagulation sedimentation-sand filtration treatment mainly for small-scale water supply. . However, when the water treatment is performed using the membrane filtration treatment, if the operation is continued,
The following phenomena occur due to suspended substances and organic substances in raw water introduced into the membrane filtration treatment as membrane supply water. That is, the surface of the membrane or the inside of the pores becomes soiled with time, and the amount of membrane filtration water decreases, or the transmembrane pressure increases.
【０００３】このように膜面あるいは細孔内が汚れた場
合には、通常、物理的洗浄法によって定期的に洗浄され
ている。物理的洗浄法としては、例えば、膜ろ過水を逆
流させる逆圧水洗浄、膜の一次側での水洗によるフラッ
シング、および膜の二次側から加圧空気を通す逆圧空気
洗浄等の方法が挙げられる。これらの方法は、膜表面の
付着屑、目詰まり、および固形物等による流路閉塞等の
ファウリングによる性能低下の回復に有効であり、一般
的には、運転時間１０〜１２０分に１回程度の頻度で洗
浄が行なわれている。さらに、従来例の特開平８−２２
９５９２号公報には、膜ろ過水をオゾン処理し、得られ
たオゾン処理水を膜ろ過装置のろ過水側から供給して膜
を逆流洗浄する方法が提案されている。[0003] When the membrane surface or the inside of the pores is contaminated as described above, it is usually cleaned regularly by a physical cleaning method. As the physical cleaning method, for example, a method of back-pressure water cleaning in which membrane filtered water flows backward, a method of flushing by water washing on a primary side of the membrane, and a method of back-pressure air cleaning in which pressurized air is passed from the secondary side of the membrane. No. These methods are effective in recovering performance deterioration due to fouling such as adhesion debris on the membrane surface, clogging, and blockage of a flow path by solid matter, and generally, once every 10 to 120 minutes of operation time. Cleaning is performed at a frequency as low as possible. Further, Japanese Patent Application Laid-Open No. Hei 8-22
No. 9592 proposes a method of subjecting membrane-filtered water to ozone treatment and supplying the obtained ozone-treated water from the filtrate water side of a membrane filtration device to backwash the membrane.
【０００４】[0004]
【発明が解決しようとする課題】湖沼水およびダム湖下
流の表流水等は、通常は５０度以下の比較的低濁度で安
定しているが、一般河川表流水等は年に数日の割合で２
５０〜５００度程度の高濁度になることがある。したが
って、原水の濁度が高くなった場合には、上述したよう
な処理プロセスにおいて次のような問題が発生するた
め、高濁度時に対処することができない。Lake water and surface water downstream of a dam lake are usually stable with relatively low turbidity of less than 50 degrees, but surface water of general rivers is several days a year. 2 by percentage
The turbidity may be as high as about 50 to 500 degrees. Therefore, when the turbidity of the raw water increases, the following problem occurs in the above-described treatment process, and it is not possible to cope with the high turbidity.
【０００５】（１）膜ろ過装置へ供給された被処理水の
濁度が高くなり、膜ろ過処理に係る負荷が増大し、膜目
詰まりが急激に進行する。[0005] (1) The turbidity of the water to be treated supplied to the membrane filtration device increases, the load involved in the membrane filtration process increases, and membrane clogging proceeds rapidly.
【０００６】（２）濁度の上昇に伴なって、原水中に含
まれる溶解性有機炭素（ＤＯＣ）等に代表される有機物
量も増加する。その結果、膜ろ過水中に所定濃度のオゾ
ンを残留させるためには、多量のオゾンを注入しなけれ
ばならず、経済的でない。さらに、場合によっては膜ろ
過水中の残留オゾンがなくなってしまうため、膜目詰ま
りが進行する。(2) As the turbidity increases, the amount of organic substances such as soluble organic carbon (DOC) contained in raw water also increases. As a result, a large amount of ozone must be injected to leave a predetermined concentration of ozone in the membrane filtration water, which is not economical. Further, in some cases, the remaining ozone in the membrane filtration water disappears, so that membrane clogging proceeds.
【０００７】本発明は、上述したような問題点を克服す
べく、鋭意検討の結果完成されたものであって、オゾン
処理と膜ろ過処理とを含む水処理方法であって、原水の
濁度が上昇した場合でも、オゾン注入量を増大させるこ
となく、しかも膜目詰まりを抑制して安定した処理水量
を得ることが可能な水処理方法を提供することを目的と
する。The present invention has been completed as a result of intensive studies in order to overcome the above-mentioned problems, and is a water treatment method including an ozone treatment and a membrane filtration treatment. It is an object of the present invention to provide a water treatment method capable of obtaining a stable amount of treated water without increasing the amount of injected ozone and suppressing film clogging even when the amount of ozone is increased.
【０００８】また本発明は、オゾン処理装置と膜ろ過処
理装置とを含む水処理装置であって、原水の濁度が上昇
した場合でも、オゾン注入量が増大せず、しかも膜目詰
まりを抑制して安定した処理水量を得ることが可能な水
処理装置を提供することを目的とする。Further, the present invention is a water treatment apparatus including an ozone treatment apparatus and a membrane filtration treatment apparatus, wherein even when the turbidity of raw water increases, the amount of injected ozone does not increase and the membrane is prevented from being clogged. It is an object of the present invention to provide a water treatment apparatus capable of obtaining a stable amount of treated water.
【０００９】[0009]
【課題を解決するための手段】上記課題を解決するため
に、本発明は、原水の濁度を低下させて除濁原水を得る
工程と、前記除濁原水を膜ろ過装置に通過させて膜ろ過
水を得る工程と、前記膜ろ過水の一部にオゾンを注入し
てオゾン処理水を得る工程と、前記オゾン処理水を用い
て、前記膜ろ過装置の膜を逆流洗浄する工程とを具備す
ることを特徴とする水処理方法を提供する。Means for Solving the Problems To solve the above problems, the present invention provides a process for reducing the turbidity of raw water to obtain turbid raw water, and passing the clarified raw water through a membrane filtration device. A step of obtaining filtered water, a step of injecting ozone into a part of the membrane filtered water to obtain ozone-treated water, and a step of backwashing the membrane of the membrane filtration device using the ozone-treated water. A water treatment method is provided.
【００１０】また本発明は、原水の濁度を低減して除濁
原水を得る装置と、前記除濁原水から膜ろ過水を得る膜
ろ過装置と、オゾン処理水を得るために前記膜ろ過水の
一部にオゾンを注入するオゾン注入装置と、前記オゾン
処理水を前記膜ろ過装置のろ過水側に供給する手段とを
具備する水処理装置を提供する。[0010] The present invention also provides an apparatus for obtaining turbid raw water by reducing turbidity of raw water, a membrane filtration apparatus for obtaining membrane filtration water from the opaque raw water, and a membrane filtration water for obtaining ozonized water. And a means for supplying the ozone-treated water to the filtered water side of the membrane filtration device.
【００１１】本発明の水処理方法においては、前記オゾ
ン処理水中の残留オゾン濃度を０．０１〜１０ｍｇ／Ｌ
にすることが好ましい。[0011] In the water treatment method of the present invention, the concentration of residual ozone in the ozonated water is 0.01 to 10 mg / L.
Is preferable.
【００１２】また本発明の水処理方法においては、前記
除濁原水の濁度を１００度以下にすることが好ましい。[0012] In the water treatment method of the present invention, it is preferable that the turbidity of the turbid raw water is 100 degrees or less.
【００１３】[0013]
【発明の実施の形態】以下、本発明の水処理方法を、図
面を参照して詳細に説明する。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Hereinafter, a water treatment method of the present invention will be described in detail with reference to the drawings.
【００１４】図１は、本発明の水処理方法の一例を説明
するための処理フローを示す図である。本発明の水処理
方法は、こうした構成の本発明の処理装置を用いて実施
することができる。FIG. 1 is a diagram showing a processing flow for explaining an example of the water treatment method of the present invention. The water treatment method of the present invention can be carried out using the treatment apparatus of the present invention having such a configuration.
【００１５】図示する装置においては、原水１は原水槽
２に供給され、ポンプ３により原水槽２から導出され
て、前処理装置としての傾斜式除濁装置４へ送り込まれ
る。ここで除濁された処理水は、処理水槽６へ導入され
た後、供給ポンプ７によって循環槽または膜供給槽８に
供給される。処理水は、その後、膜供給ポンプ９から膜
ろ過装置１０に送り込まれる。In the illustrated apparatus, raw water 1 is supplied to a raw water tank 2, taken out of the raw water tank 2 by a pump 3, and sent to an inclined clarifier 4 as a pretreatment device. The treated water that has been clarified here is introduced into the treated water tank 6 and then supplied to the circulation tank or the membrane supply tank 8 by the supply pump 7. The treated water is then sent from the membrane supply pump 9 to the membrane filtration device 10.
【００１６】膜ろ過装置１０において得られた膜ろ過水
１２は、膜ろ過水槽１３へ送り込まれ、膜ろ過水の一部
１５は膜逆流洗浄水として用いるために逆洗水槽１６へ
導入されて、残りの大部分は処理水１４として得られ
る。膜ろ過水の一部１５が導入される逆洗水槽１６内に
は散気管１９が設置されており、この散気管１９からオ
ゾン発生器１７で生成されたオゾン１８が吹き込まれ
る。それによって、処理水は所定のオゾン濃度になるよ
うにオゾン処理される。The membrane filtration water 12 obtained in the membrane filtration device 10 is sent to a membrane filtration water tank 13, and a part 15 of the membrane filtration water is introduced into a backwash water tank 16 for use as membrane backwash water. Most of the rest is obtained as treated water 14. A diffuser pipe 19 is provided in a backwash water tank 16 into which a part 15 of the membrane filtered water is introduced, and ozone 18 generated by an ozone generator 17 is blown from the diffuser pipe 19. Thereby, the treated water is ozone-treated so as to have a predetermined ozone concentration.
【００１７】このようにして得られたオゾン処理水２０
は、膜の逆流洗浄のタイミングに合わせて逆洗ポンプ２
１により逆洗水槽１６から導出され、膜ろ過装置１０の
ろ過水側から圧入して逆洗させる。こうして、膜の汚れ
や目詰まり物質を効果的に除去することができる。The ozone-treated water 20 thus obtained is
Is the backwash pump 2 according to the timing of backwashing of the membrane.
The water is drawn out of the backwash water tank 16 by 1 and press-fitted from the filtered water side of the membrane filtration device 10 to backwash. Thus, dirt and clogging substances on the film can be effectively removed.
【００１８】なお、図示していないが、逆洗水槽１６中
にオゾン検出器を設け、このオゾン検出器により逆洗水
槽中の残留オゾン濃度を検出して、吹き込みオゾン注入
量を制御することもできる。また、膜ろ過装置１０にお
いて循環水１１を循環槽または膜供給槽８へ返送するこ
ともできる。Although not shown, an ozone detector may be provided in the backwash water tank 16, and the ozone detector may detect the concentration of residual ozone in the backwash water tank to control the amount of injected ozone. it can. Further, the circulating water 11 can be returned to the circulation tank or the membrane supply tank 8 in the membrane filtration device 10.
【００１９】逆洗水槽１６内でオゾン処理を施すに当た
っては、通常の散気管方式による注入形式が好ましい
が、インジェクター式、エジェクター式、および下降注
入式等のいずれの形式でも可能である。オゾン処理にお
けるオゾン吹き込み量は、被処理水の水質に応じて任意
に選択できるが、０．０１〜１０ｍｇ／Ｌとすることが
好ましく、０．１〜７．０ｍｇ／Ｌとすることがより好
ましい。オゾン処理水中の残留オゾン濃度が１０ｍｇ／
Ｌより高くなると、膜ろ過装置１０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
により膜劣化が起こるおそれがあるものの、膜モジュー
ルの交換時期を考え合わせると、１０ｍｇ／Ｌまでは許
容される。また、残留オゾン濃度が１０ｍｇ／Ｌより高
くなると、副生成物量も多くなるという問題がある。以
上のことから、膜ろ過水中の残留オゾン濃度は、０．０
１〜１０ｍｇ／Ｌであることが好ましく、０．１〜７．
０ｍｇ／Ｌであることがより好ましい。In performing the ozone treatment in the backwash water tank 16, an injection method using a normal air diffuser is preferable, but any type such as an injector type, an ejector type, and a downward injection type can be used. The amount of ozone blown in the ozone treatment can be arbitrarily selected according to the quality of the water to be treated, but is preferably 0.01 to 10 mg / L, more preferably 0.1 to 7.0 mg / L. . The residual ozone concentration in the ozonated water is 10 mg /
If it is higher than L, even if an ozone-resistant membrane material is used as the filtration membrane of the membrane filtration device 10, there is a possibility that the membrane will deteriorate due to the reaction with ozone in the long term, but the exchange time of the membrane module is considered. And up to 10 mg / L are acceptable. Further, when the residual ozone concentration is higher than 10 mg / L, there is a problem that the amount of by-products increases. From the above, the residual ozone concentration in the membrane filtration water is 0.0
It is preferably 1 to 10 mg / L, and 0.1 to 7 mg / L.
More preferably, it is 0 mg / L.
【００２０】ここで、図１に示した処理装置における前
処理装置としての傾斜式除濁装置４について詳細に説明
する。図２に、傾斜式除濁装置４の詳細を示す。Here, the tilt type clarifier 4 as a pretreatment device in the treatment device shown in FIG. 1 will be described in detail. FIG. 2 shows details of the tilt type clarifier 4.
【００２１】図示するように、傾斜式除濁装置４は、急
速攪拌槽３２、緩速攪拌槽３４および沈殿装置３５より
構成されている。As shown in the figure, the tilt type clarifier 4 comprises a rapid stirring tank 32, a slow stirring tank 34, and a sedimentation device 35.
【００２２】急速攪拌槽３２には、原水槽からの原水が
供給ポンプ３を介して導入され、さらに凝集剤３０が添
加される。原水と凝集剤３０とは、急速攪拌機３１によ
って急速攪拌され、その後、緩速攪拌槽３４に導かれ
る。Raw water from the raw water tank is introduced into the rapid stirring tank 32 through the supply pump 3, and the coagulant 30 is further added. The raw water and the flocculant 30 are rapidly stirred by the rapid stirrer 31 and then guided to the slow stirring tank 34.
【００２３】緩速攪拌槽３４においては、薬剤を伴なっ
た原水を緩速攪拌機３３によって緩速攪拌して凝集フロ
ックを形成し、生じた凝集フロックおよび原水は沈殿装
置３５に導入される。In the slow stirring tank 34, the raw water with the chemicals is slowly stirred by the slow stirring machine 33 to form flocculated flocs. The generated flocculated flocs and raw water are introduced into the precipitation device 35.
【００２４】この沈殿装置３５は、傾斜装置３６を有し
ており、傾斜装置３６に上向流（例えば２０ｍ／ｈ）で
通水して、濁質の凝集フロックを沈降分離する。傾斜装
置３６は、傾斜管若しくは傾斜板を、上向流に対して所
定角度に傾斜して配置したものである。濁質の凝集フロ
ックが沈降分離されるので、処理水槽６には、濁度の低
減された原水が導入される。The sedimentation device 35 has a tilting device 36, and water is passed through the tilting device 36 in an upward flow (for example, 20 m / h) to settle and separate suspended floc. The inclining device 36 is configured such that an inclining tube or an inclining plate is arranged to be inclined at a predetermined angle with respect to the upward flow. Since the flocculated floc of the turbid matter is settled and separated, raw water with reduced turbidity is introduced into the treated water tank 6.
【００２５】こうした構成を有する傾斜式除濁装置を用
いることによって、原水濁度が大きく変動した場合にお
いても、膜ろ過装置に供給する前に、常に濁度を１００
度以下まで低下させることができる。By using the inclined type turbidity separator having such a configuration, even when the turbidity of the raw water fluctuates greatly, the turbidity is always kept at 100% before being supplied to the membrane filtration device.
Degrees or less.
【００２６】ここで濁度を１００度以下としているの
は、膜ろ過処理に係る負荷を軽減することによる目詰ま
りの抑制を考慮したためである。Here, the reason why the turbidity is set to 100 degrees or less is to suppress clogging by reducing the load relating to the membrane filtration treatment.
【００２７】次に、本発明において用いられる膜ろ過装
置１０について説明する。膜ろ過装置１０は、膜供給水
にオゾンが溶解された状態で膜ろ過するために、生物フ
ァウリングによる膜の目詰まりを防止することができ、
かつ高い透過流束を得ることが可能である。膜ろ過装置
１０に使用される膜は、原水中の濁質成分および細菌類
を除去することのできる膜であり、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、公称孔径
０．０１〜０．５μｍのものが用いられ、限外ろ過膜の
場合には、分画分子量１，０００〜２０万ダルトンのも
のが用いられる。また、膜モジュールの形式は、中空糸
状、スパイラル状、チューブラ状、および平膜状等のい
ずれの形式でも問題はない。膜素材およびポッティング
部は、高濃度のオゾンと接触するために、耐オゾン性の
素材で構成することが望ましい。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、膜モジュールのろ過方式は、全量ろ過方式およびク
ロスフローろ過方式のいずれの方式を用いてもよい。さ
らに、膜ろ過への通水方式は、外圧型と内圧型があり、
どちらの通水方式でも問題ない。Next, the membrane filtration device 10 used in the present invention will be described. The membrane filtration device 10 can prevent membrane clogging due to biological fouling because the membrane filtration is performed in a state where ozone is dissolved in the membrane supply water,
And it is possible to obtain a high permeation flux. The membrane used in the membrane filtration device 10 is a membrane capable of removing turbid components and bacteria in raw water, and a microfiltration membrane or an ultrafiltration membrane is used. In the case of a microfiltration membrane, one having a nominal pore size of 0.01 to 0.5 μm is used, and in the case of an ultrafiltration membrane, one having a molecular weight cut off of 1,000 to 200,000 daltons is used. The type of the membrane module may be any type such as a hollow fiber shape, a spiral shape, a tubular shape, and a flat membrane shape. It is desirable that the film material and the potting portion be made of an ozone-resistant material in order to come into contact with high-concentration ozone. 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. Further, as the filtration method of the membrane module, any of a total filtration method and a cross-flow filtration method may be used. In addition, there are external pressure type and internal pressure type,
There is no problem with either water flow method.
【００２８】以上、原水の濁度を低減するための前処理
装置として傾斜式除濁装置を用いた例を説明したが、本
発明の方法においては、他の装置を用いて原水の濁度を
低減することもできる。図３には、傾斜式除濁装置に換
えて生物接触ろ過装置を用いた例を示す。The above description has been given of the example in which the inclined clarifier is used as the pretreatment device for reducing the turbidity of the raw water. However, in the method of the present invention, the turbidity of the raw water is reduced by using another device. It can also be reduced. FIG. 3 shows an example in which a biological contact filtration device is used in place of the tilt type clarifier.
【００２９】図示する処理装置は、前処理装置として生
物接触ろ過装置５を用いること以外は、図１に示した装
置と同様である。すなわち、原水１は原水槽２に供給さ
れ、ポンプ３により原水槽２から導出されて、前処理装
置としての生物接触ろ過装置５へ送り込まれる。ここで
除濁された処理水は、処理水槽６へ導入された後、供給
ポンプ７によって循環槽または膜供給槽８に供給され
る。処理水は、その後、膜供給ポンプ９から膜ろ過装置
１０に送り込まれる。The illustrated processing apparatus is the same as the apparatus shown in FIG. 1 except that a biological contact filtration device 5 is used as a pretreatment device. That is, the raw water 1 is supplied to the raw water tank 2, extracted from the raw water tank 2 by the pump 3, and sent to the biological contact filtration device 5 as a pretreatment device. The treated water that has been clarified here is introduced into the treated water tank 6 and then supplied to the circulation tank or the membrane supply tank 8 by the supply pump 7. The treated water is then sent from the membrane supply pump 9 to the membrane filtration device 10.
【００３０】膜ろ過装置１０において得られた膜ろ過水
１２は、膜ろ過水槽１３へ送り込まれ、膜ろ過水の一部
１５は膜逆流洗浄水として用いるために逆洗水槽１６へ
導入され、残りの大部分は処理水１４として得られる。
膜ろ過水の一部１５が導入される逆洗水槽１６内には散
気管１９が設置されており、この散気管１９からオゾン
発生器１７で生成されたオゾン１８が吹き込まれる。そ
れによって、処理水は所定のオゾン濃度になるようにオ
ゾン処理される。The membrane filtration water 12 obtained in the membrane filtration device 10 is sent to a membrane filtration water tank 13, and a part 15 of the membrane filtration water is introduced into a backwash water tank 16 for use as membrane backwash water, and the remaining water is removed. Is obtained as treated water 14.
A diffuser pipe 19 is provided in a backwash water tank 16 into which a part 15 of the membrane filtered water is introduced, and ozone 18 generated by an ozone generator 17 is blown from the diffuser pipe 19. Thereby, the treated water is ozone-treated so as to have a predetermined ozone concentration.
【００３１】このようにして得られたオゾン処理水２０
は、膜の逆流洗浄のタイミングに合わせて逆洗ポンプ２
１により逆洗水槽１６から導出され、膜ろ過装置１０の
ろ過水側から圧入して逆洗させる。こうして、膜の汚れ
や目詰まり物質を効果的に除去することができる。The ozone-treated water 20 thus obtained is
Is the backwash pump 2 according to the timing of backwashing of the membrane.
The water is drawn out of the backwash water tank 16 by 1 and press-fitted from the filtered water side of the membrane filtration device 10 to backwash. Thus, dirt and clogging substances on the film can be effectively removed.
【００３２】なお、図示していないが、逆洗水槽１６中
にオゾン検出器を設け、このオゾン検出器により逆洗水
槽中の残留オゾン濃度を検出して、吹き込みオゾン注入
量を制御することもできる。また、膜ろ過装置１０にお
いて循環水１１を循環槽または膜供給槽８へ返送するこ
ともできる。Although not shown, an ozone detector may be provided in the backwash water tank 16, and the ozone detector may detect the residual ozone concentration in the backwash water tank to control the amount of injected ozone. it can. Further, the circulating water 11 can be returned to the circulation tank or the membrane supply tank 8 in the membrane filtration device 10.
【００３３】ここで、図３に示した処理装置における前
処理装置としての生物接触ろ過装置５について説明す
る。この生物接触ろ過装置５は、微生物を担持したろ材
を所定の層厚で塔内に充填したものである。ろ材に担持
された微生物によって原水水質の平準化、アンモニア性
窒素の硝化および生物易分解性有機物の低減が行なわれ
るとともに、ろ材の有するろ過機能により原水の濁度が
除去されるので、生物処理機能と濁質捕捉機能とを兼ね
ている。ろ材の構成は、上段充填層および下段充填層と
いった複層構成としても問題はない。Here, a biological contact filtration device 5 as a pretreatment device in the treatment device shown in FIG. 3 will be described. This biological contact filtration device 5 is one in which a filter medium carrying microorganisms is packed in a tower with a predetermined layer thickness. The microorganisms carried on the filter media level the raw water quality, nitrify ammonia nitrogen and reduce biodegradable organic matter, and remove the turbidity of the raw water by the filtration function of the filter media. And the turbidity trapping function. There is no problem even if the structure of the filter medium is a multi-layer structure such as an upper packing layer and a lower packing layer.
【００３４】こうした構成を有する生物接触ろ過装置を
用いることによって、原水濁度が大きく変動した場合に
おいても、膜ろ過装置に供給する前に、常に濁度を１０
０度以下まで低下させることができる。By using the biological contact filtration device having such a configuration, even when the turbidity of the raw water fluctuates greatly, the turbidity is always reduced to 10 before being supplied to the membrane filtration device.
It can be reduced to 0 degrees or less.
【００３５】さらに、本発明の方法においては、原水の
濁度を低減するための前処理装置として、安価でかつ維
持管理性の優れたオートストレーナを用いて原水の濁度
を低減することもできる。この場合、目開きは１００μ
ｍ〜数ｎｍのサイズのものが好ましい。Further, in the method of the present invention, the turbidity of the raw water can be reduced by using an inexpensive auto-strainer having excellent maintainability as a pretreatment device for reducing the turbidity of the raw water. . In this case, the aperture is 100μ
Those having a size of m to several nm are preferred.
【００３６】[0036]
【実施例】以下、本発明に基づく汚水の処理方法および
処理装置の実施例について説明する。なお、以下の実施
例は本発明に限定を加えるものではない。DESCRIPTION OF THE PREFERRED EMBODIMENTS Embodiments of a wastewater treatment method and treatment apparatus according to the present invention will be described below. The following examples do not limit the present invention.
【００３７】（実施例１）図１に示した本発明の処理フ
ローに基づく実験装置（処理量３５ｍ3／日）におい
て、河川表流水を原水として処理実験を行なった。(Example 1) In an experimental apparatus (a processing amount of 35 m 3 / day) based on the processing flow of the present invention shown in FIG. 1, a processing experiment was performed using river surface water as raw water.
【００３８】傾斜式除濁装置４には、凝集剤３０として
ポリ塩化アルミニウム（ＰＡＣ）溶液を２０ｍｇ／Ｌ添
加した。膜ろ過装置１０には、公称孔径０．１μｍのフ
ッ化ビニリデン重合体樹脂製精密ろ過膜（膜面積７ｍ2
の中空糸膜）を適用して、デッドエンドろ過にて設定フ
ラックス２ｍ3／ｍ2／日の定流量ろ過運転を行なった。A polyaluminum chloride (PAC) solution (20 mg / L) was added as a flocculant 30 to the inclined turbidity removing device 4. The membrane filtration device 10 is provided with a vinylidene fluoride polymer resin microfiltration membrane (membrane area 7 m 2) having a nominal pore size of 0.1 μm.
And a constant flow filtration operation with a set flux of 2 m 3 / m 2 / day was performed by dead end filtration.
【００３９】運転条件は、ろ過を２０分間行なった後、
逆流洗浄を３０秒間行なうという操作を繰り返し、２時
間毎に膜モジュール直下から空気を供給してエアーバブ
リングを２分間行なった。また、逆洗水槽１６における
残留オゾン濃度が５ｍｇ／Ｌ程度となるように、散気管
方式でオゾン１８を注入してオゾン処理を行なった。The operating conditions are as follows: after performing filtration for 20 minutes,
The operation of performing backwashing for 30 seconds was repeated, and air was bubbled from immediately below the membrane module every 2 hours to perform air bubbling for 2 minutes. Further, ozone 18 was injected by an air diffusion tube method to perform ozone treatment so that the residual ozone concentration in the backwash water tank 16 was about 5 mg / L.
【００４０】図４のグラフに、原水および傾斜式除濁装
置処理水における濁度の経時変化を示す。また、膜ろ過
装置１０における膜間差圧（２５℃換算）の経時変化
は、図５のグラフに示した通りである。FIG. 4 is a graph showing the change over time in the turbidity of the raw water and the treated water of the inclined type clarifier. In addition, the change with time of the transmembrane pressure (converted to 25 ° C.) in the membrane filtration device 10 is as shown in the graph of FIG.
【００４１】図４のグラフに示されるように、本発明の
処理フローで処理することによって、原水濁度が高くな
った場合においても傾斜式除濁装置処理水の濃度は常に
３０度以下に抑えることができる。また、フラックス２
ｍ3／ｍ2／日の条件において、約３ヶ月にわたって膜間
差圧の上昇もなく安定して通水することができること
が、図５のグラフから明らかである。As shown in the graph of FIG. 4, the concentration in the treated water of the inclined type clarifier is always suppressed to 30 degrees or less even when the turbidity of the raw water is increased by treating with the treatment flow of the present invention. be able to. In addition, flux 2
It is clear from the graph of FIG. 5 that under the condition of m 3 / m 2 / day, water can be stably passed without increasing the transmembrane pressure for about 3 months.
【００４２】（実施例２）図３に示した本発明の処理フ
ローに基づく実験装置（処理量３５ｍ3／日）におい
て、河川表流水を原水として処理実験を行なった。(Example 2) In an experimental apparatus (a processing amount of 35 m 3 / day) based on the processing flow of the present invention shown in FIG. 3, a processing experiment was performed using river surface water as raw water.
【００４３】生物接触ろ過装置５においては、ろ材の構
成を２層構成とし、上段充填層にポリプロピレン製の中
空円筒状のろ材（φ４ｍｍ×Ｌ５ｍｍ）を用い、下段充
填層にはセラミック製の球形のろ材（有効径１ｍｍ）を
用いた。In the biological contact filtration device 5, the filter medium has a two-layer structure, a hollow cylindrical filter medium (φ4 mm × L5 mm) made of polypropylene is used for the upper packing layer, and a ceramic spherical filter is used for the lower packing layer. A filter medium (effective diameter 1 mm) was used.
【００４４】膜ろ過装置１０における仕様および運転条
件は、実施例１の場合と同様とした。さらに、逆洗水槽
１６における残留オゾン濃度が５ｍｇ／Ｌ程度となるよ
うに散気管方式でオゾン１８を注入してオゾン処理を行
なった。The specifications and operating conditions of the membrane filtration device 10 were the same as those in Example 1. Further, ozone treatment was performed by injecting ozone 18 by a diffuser method so that the residual ozone concentration in the backwash water tank 16 was about 5 mg / L.
【００４５】図４のグラフに、原水および生物接触ろ過
装置処理水における濁度の経時変化を示す。また、膜ろ
過装置１０における膜間差圧（２５℃換算）の経時変化
は、図５のグラフに示した通りである。FIG. 4 is a graph showing the change over time in the turbidity of the raw water and the treated water of the biological contact filtration device. In addition, the change with time of the transmembrane pressure (converted to 25 ° C.) in the membrane filtration device 10 is as shown in the graph of FIG.
【００４６】図４のグラフに示されるように、本発明の
処理フローで処理することによって、原水濁度が高くな
った場合においても、生物接触ろ過装置処理水の濃度は
常に５０度以下に抑えることができる。また、フラック
ス５ｍ3／ｍ2／日の条件において、約３ヶ月にわたって
膜間差圧の上昇もなく安定して通水することができるこ
とが図５のグラフから明らかである。As shown in the graph of FIG. 4, even when the raw water turbidity is increased by the treatment according to the treatment flow of the present invention, the concentration of the treated water in the biological contact filtration device is always suppressed to 50 ° or less. be able to. In addition, it is clear from the graph of FIG. 5 that under the condition of a flux of 5 m 3 / m 2 / day, water can be stably passed without an increase in transmembrane pressure for about 3 months.
【００４７】（比較例１）実施例１において前処理装置
を設置することなく、原水を膜ろ過装置１０へ直接供給
する処理フローにおいて、河川表流水を原水として処理
実験を行なった。(Comparative Example 1) In Example 1, a processing experiment was performed using river surface water as raw water in a processing flow of directly supplying raw water to the membrane filtration device 10 without installing a pretreatment device.
【００４８】膜ろ過装置１０における仕様および運転条
件は、実施例１の場合と同様とした。また、逆洗水槽１
６における残留オゾン濃度が５ｍｇ／Ｌ程度となるよう
に散気管方式でオゾン１８を注入してオゾン処理を行な
った。The specifications and operating conditions of the membrane filtration device 10 were the same as those in the first embodiment. In addition, backwash water tank 1
Ozone 18 was injected by a diffuser method so that the residual ozone concentration in No. 6 was about 5 mg / L, and ozone treatment was performed.
【００４９】図４のグラフに、原水における濁度の経時
変化を示す。また、膜ろ過装置１０における膜間差圧
（２５℃換算）の経時変化は、図５のグラフに示した通
りである。FIG. 4 is a graph showing the change over time in the turbidity of the raw water. In addition, the change with time of the transmembrane pressure (converted to 25 ° C.) in the membrane filtration device 10 is as shown in the graph of FIG.
【００５０】図４および図５のグラフに示されるよう
に、原水濁度の上昇に伴なって膜間差圧も上昇する傾向
にある。これは、膜面あるいは細孔内に付着した無機物
等によって膜目詰まりが次第に進行したためであり、フ
ラックス２ｍ3／ｍ2／日の条件においては、約２ヶ月で
膜の薬品洗浄を行なうに至った。As shown in the graphs of FIGS. 4 and 5, as the raw water turbidity increases, the transmembrane pressure tends to increase. This is because film clogging gradually progressed due to inorganic substances or the like adhering to the film surface or in the pores. Under conditions of a flux of 2 m 3 / m 2 / day, chemical cleaning of the film was performed in about 2 months. Was.
【００５１】[0051]
【発明の効果】以上説明したように本発明によれば、オ
ゾン処理と膜ろ過処理とを含む水処理方法であって、原
水の濁度が上昇した場合でも、オゾン注入量を増大させ
ることなく、しかも膜目詰まりを抑制して安定した処理
水量を得ることが可能な水処理方法が提供される。ま
た、本発明によれば、オゾン処理装置と膜ろ過処理装置
とを含む水処理装置であって、原水の濁度が上昇した場
合でも、オゾン注入量が増大せず、しかも膜目詰まりを
抑制して安定した処理水量を得ることが可能な水処理装
置が提供される。As described above, according to the present invention, there is provided a water treatment method including an ozone treatment and a membrane filtration treatment, wherein the ozone injection amount is not increased even when the turbidity of the raw water increases. Further, there is provided a water treatment method capable of suppressing membrane clogging and obtaining a stable treated water amount. Further, according to the present invention, there is provided a water treatment apparatus including an ozone treatment apparatus and a membrane filtration treatment apparatus, wherein even when the turbidity of raw water increases, the ozone injection amount does not increase and furthermore, membrane clogging is suppressed. And a water treatment apparatus capable of obtaining a stable amount of treated water.
【００５２】本発明を用いることにより、高い膜透過流
束においても膜の目詰まりを大幅に軽減することがで
き、膜の目詰まりに対処するための薬品洗浄に要する労
力と洗浄用薬剤費とを低減することができる。しかも、
オゾンの注入制御を行なうことによって、オゾン注入量
を最小限にして無駄なオゾン消費を抑制することが可能
となる。本発明は、上水道、下水道、工業用水または廃
水の処理に極めて有効に用いられ、その工業的価値は大
きい。By using the present invention, clogging of a membrane can be greatly reduced even at a high membrane permeation flux, and the labor required for chemical cleaning to cope with membrane clogging and the cost of cleaning chemicals are reduced. Can be reduced. Moreover,
By performing ozone injection control, it becomes possible to minimize wasteful ozone consumption by minimizing the ozone injection amount. INDUSTRIAL APPLICABILITY The present invention is very effectively used for water supply, sewerage, industrial water or wastewater treatment, and has great industrial value.
【図１】本発明の一実施例の処理フローを示す図。FIG. 1 is a diagram showing a processing flow of an embodiment of the present invention.
【図２】本発明に用いられる傾斜式除濁装置の構成を示
す概略図。FIG. 2 is a schematic view showing a configuration of a tilt type clarifier used in the present invention.
【図３】本発明の他の実施例の処理フローを示す図。FIG. 3 is a diagram showing a processing flow of another embodiment of the present invention.
【図４】濁度の経時変化を示すグラフ図。FIG. 4 is a graph showing changes over time in turbidity.
【図５】膜間差圧の経時変化を示すグラフ図。FIG. 5 is a graph showing a temporal change of a transmembrane pressure difference.
１…原水 ２…原水槽 ３…供給ポンプ ４…傾斜式除濁装置 ５…生物接触ろ過装置 ６…処理水槽 ７…供給ポンプ ８…循環槽または膜供給槽 ９…膜供給ポンプ １０…膜ろ過装置 １１…循環水 １２…膜ろ過水 １３…膜ろ過水槽 １４…処理水 １５…膜ろ過水 １６…逆洗水槽 １７…オゾン発生器 １８…オゾンガス １９…散気管 ２０…オゾン処理水 ２１…逆洗ポンプ ３０…凝集剤 ３１…急速攪拌機 ３２…急速攪拌槽 ３３…緩速攪拌機 ３４…緩速攪拌槽 ３５…沈殿装置 ３６…傾斜装置 DESCRIPTION OF SYMBOLS 1 ... Raw water 2 ... Raw water tank 3 ... Supply pump 4 ... Inclined clarifier 5 ... Biological contact filtration apparatus 6 ... Treatment water tank 7 ... Supply pump 8 ... Circulation tank or membrane supply tank 9 ... Membrane supply pump 10 ... Membrane filtration apparatus DESCRIPTION OF SYMBOLS 11 ... Circulating water 12 ... Membrane filtration water 13 ... Membrane filtration water tank 14 ... Treated water 15 ... Membrane filtration water 16 ... Backwashing water tank 17 ... Ozone generator 18 ... Ozone gas 19 ... Aeration tube 20 ... Ozonized water 21 ... Backwashing pump DESCRIPTION OF SYMBOLS 30 ... Coagulant 31 ... Rapid stirring machine 32 ... Rapid stirring tank 33 ... Slow stirring machine 34 ... Slow stirring tank 35 ... Precipitation apparatus 36 ... Incliner
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｃ０２Ｆ 1/44 Ｃ０２Ｆ 1/44 Ｈ Ｋ 1/52 1/52 Ｚ 1/78 1/78 3/06 3/06 9/00 ５０１ 9/00 ５０１Ｂ ５０２ ５０２Ｐ ５０２Ｒ ５０２Ｅ ５０３ ５０３Ａ ５０３Ｃ ５０３Ｇ ５０４ ５０４Ｄ ５０４Ｅ (71)出願人 000005234 富士電機株式会社 神奈川県川崎市川崎区田辺新田１番１号 (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 森 吉彦 静岡県富士市鮫島２−１ 旭化成工業株式 会社内 (72)発明者 橋野 昌年 静岡県富士市鮫島２−１ 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 高橋 和孝 神奈川県川崎市川崎区田辺新田１番１号 富士電機株式会社内 (72)発明者 角川 功明 神奈川県川崎市川崎区田辺新田１番１号 富士電機株式会社内 Ｆターム(参考） 4D003 AA01 BA02 CA02 CA10 EA01 EA15 EA24 EA30 FA02 4D006 GA06 GA07 HA01 HA21 HA41 HA61 HA95 KA02 KA12 KA42 KA71 KB13 KB25 KB30 KC03 KC16 KD21 MA01 MA02 MA03 MA22 MB05 MC03 MC29 PA01 PB02 PB08 PB24 4D050 AA01 AA12 AA13 AB06 AB11 BB02 BD03 BD08 CA09 CA16 CA17 4D062 BA29 BB05 CA01 CA14 DA04 EA04 EA07 EA32 FA02 FA17 FA24 ──────────────────────────────────────────────────の Continued on the front page (51) Int.Cl. 7 Identification code FI Theme coat ゛ (Reference) C02F 1/44 C02F 1/44 H K 1/52 1/52 Z 1/78 1/78 3/06 3 / 06 9/00 501 9/00 501B 502 502P 502R 502E 503 503A 503C 503G 504 504D 504E (71) Applicant 000005234 Fuji Electric Co., Ltd. 1-1-1 Tanabe Shinda, Kawasaki-ku, Kawasaki City, Kanagawa Prefecture, Japan (72) Inventor Minegishi Torataro 1-2-1, Marunouchi, Chiyoda-ku, Tokyo Nihon Kokan Co., Ltd. (72) Inventor Kenichiro Mizuno 1-2-1, Marunouchi, Chiyoda-ku, Tokyo Nihon Kokan Co., Ltd. (72) Inventor Yoshihiko Mori Shizuoka (72) Inventor Masanori Hashino 2-1 Samejima, Fuji-shi, Shizuoka Asahi Kasei Corporation (72) Kinzo Isomura, Inventor Kinzo Isomura 1-3-1, Toranomon, Minato-ku, Tokyo, Japan Yutaka Isomura Waterworks Co., Ltd. (72) Inventor Kenji Nakatani 1-3-1, Toranomon, Minato-ku, Tokyo Mizuyoshi, Isomura Kiko Co., Ltd. (72) Inventor Kazutaka Takahashi 1-1-1, Tanabe Nitta, Kawasaki-ku, Kawasaki, Kanagawa Prefecture Inside Fuji Electric Co., Ltd. (72) Inventor Tomoaki Kadokawa 1-1, Tanabe Nitta, Kawasaki-ku, Kawasaki-shi, Kanagawa F-term in Fuji Electric Co., Ltd. (reference) 4D003 AA01 BA02 CA02 CA10 EA01 EA15 EA24 EA30 FA02 4D006 GA06 GA07 HA01 HA21 HA41 HA61 HA95 KA02 KA12 KA42 KA71 KB13 KB25 KB30 KC03 KC16 KD21 MA01 MA02 MA03 MA22 MB05 MC03 PB0408 AA01 AA12 AA13 AB06 AB11 BB02 BD03 BD08 CA09 CA16 CA17 4D062 BA29 BB05 CA01 CA14 DA04 EA04 EA07 EA32 FA02 FA17 FA24
Claims (4)
工程と、 前記除濁原水を膜ろ過装置に通過させて膜ろ過水を得る
工程と、 前記膜ろ過水の一部にオゾンを注入してオゾン処理水を
得る工程と、 前記オゾン処理水を用いて、前記膜ろ過装置の膜を逆流
洗浄する工程とを具備することを特徴とする水処理方
法。A step of reducing the turbidity of the raw water to obtain turbid raw water; a step of passing the turbid raw water through a membrane filtration device to obtain membrane filtered water; And a step of backwashing the membrane of the membrane filtration device using the ozone-treated water.
０．０１〜１０ｍｇ／Ｌに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 water treatment method according to claim 1, wherein the concentration of residual ozone in the ozonated water is adjusted to 0.01 to 10 mg / L.
ることを特徴とする請求項１または２に記載の水処理方
法。3. The water treatment method according to claim 1, wherein the turbidity of the raw turbid water is set to 100 degrees or less.
置と、 前記除濁原水から膜ろ過水を得る膜ろ過装置と、 オゾン処理水を得るために前記膜ろ過水の一部にオゾン
を注入するオゾン注入装置と、 前記オゾン処理水を前記膜ろ過装置のろ過水側に供給す
る手段とを具備する水処理装置。4. An apparatus for obtaining turbid raw water by reducing the turbidity of raw water, a membrane filtration apparatus for obtaining membrane filtered water from the opaque raw water, and a part of the membrane filtered water for obtaining ozonized water. A water treatment apparatus comprising: an ozone injecting device that injects ozone into the water; and a unit that supplies the ozonized water to a filtrate side of the membrane filtration device.
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| JP2000222786A JP2002035554A (en) | 2000-07-24 | 2000-07-24 | Method for treating water and its apparatus |
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| JP2000222786A JP2002035554A (en) | 2000-07-24 | 2000-07-24 | Method for treating water and its apparatus |
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Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005205295A (en) * | 2004-01-21 | 2005-08-04 | Kokan Kogyo Kk | Method and apparatus for evaluating water quality of river |
| JP2007083155A (en) * | 2005-09-21 | 2007-04-05 | Fuji Electric Systems Co Ltd | Water treatment method |
| WO2008015939A1 (en) * | 2006-08-01 | 2008-02-07 | Metawater Co., Ltd. | Method of reutilizing wastewater |
| CN103265152A (en) * | 2013-06-14 | 2013-08-28 | 山西太钢不锈钢股份有限公司 | Domestic sewage treatment method |
| JP2014061506A (en) * | 2012-09-24 | 2014-04-10 | Hitachi Ltd | Liquid treatment facility |
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|---|---|---|---|---|
| JPH05123673A (en) * | 1991-11-08 | 1993-05-21 | Toshiba Corp | Water treating device |
| JPH07961A (en) * | 1993-06-18 | 1995-01-06 | Toshiba Corp | Water treatment device |
| JPH07213875A (en) * | 1994-02-02 | 1995-08-15 | Hitachi Plant Eng & Constr Co Ltd | Production of clear water |
| JPH08229592A (en) * | 1995-02-27 | 1996-09-10 | Kurita Water Ind Ltd | Biological water treatment |
| JPH10309576A (en) * | 1997-05-08 | 1998-11-24 | Asahi Chem Ind Co Ltd | Water treatment by ozone resistant membrane |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH05123673A (en) * | 1991-11-08 | 1993-05-21 | Toshiba Corp | Water treating device |
| JPH07961A (en) * | 1993-06-18 | 1995-01-06 | Toshiba Corp | Water treatment device |
| JPH07213875A (en) * | 1994-02-02 | 1995-08-15 | Hitachi Plant Eng & Constr Co Ltd | Production of clear water |
| JPH08229592A (en) * | 1995-02-27 | 1996-09-10 | Kurita Water Ind Ltd | Biological water treatment |
| JPH10309576A (en) * | 1997-05-08 | 1998-11-24 | Asahi Chem Ind Co Ltd | Water treatment by ozone resistant membrane |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005205295A (en) * | 2004-01-21 | 2005-08-04 | Kokan Kogyo Kk | Method and apparatus for evaluating water quality of river |
| JP2007083155A (en) * | 2005-09-21 | 2007-04-05 | Fuji Electric Systems Co Ltd | Water treatment method |
| WO2008015939A1 (en) * | 2006-08-01 | 2008-02-07 | Metawater Co., Ltd. | Method of reutilizing wastewater |
| JP5143002B2 (en) * | 2006-08-01 | 2013-02-13 | メタウォーター株式会社 | Wastewater reuse method |
| US8968569B2 (en) | 2006-08-01 | 2015-03-03 | Metawater Co., Ltd. | Method for recycling wastewater |
| JP2014061506A (en) * | 2012-09-24 | 2014-04-10 | Hitachi Ltd | Liquid treatment facility |
| CN103265152A (en) * | 2013-06-14 | 2013-08-28 | 山西太钢不锈钢股份有限公司 | Domestic sewage treatment method |
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