JP2876978B2 - Water purification method - Google Patents
Water purification methodInfo
- Publication number
- JP2876978B2 JP2876978B2 JP3099694A JP3099694A JP2876978B2 JP 2876978 B2 JP2876978 B2 JP 2876978B2 JP 3099694 A JP3099694 A JP 3099694A JP 3099694 A JP3099694 A JP 3099694A JP 2876978 B2 JP2876978 B2 JP 2876978B2
- Authority
- JP
- Japan
- Prior art keywords
- membrane
- washing
- filtration
- turbidity
- time
- 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)
Description
【０００１】[0001]
【発明の利用分野】本発明は浄水製造方法に係り、特に
精密濾過膜または限外濾過膜等の膜を用いて汚水を濾過
することにより浄水を得る浄水製造方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for producing purified water, and more particularly to a method for producing purified water by filtering wastewater using a membrane such as a microfiltration membrane or an ultrafiltration membrane.
【０００２】[0002]
【従来の技術】従来、浄水製造方法としては、凝集沈殿
工程と砂濾過工程を組み合わせ、これに殺菌あるいは塩
素処理を加えた方法が定着している。しかし、この方法
は広い設置面積を必要とするため、最近、凝集沈殿工程
及び砂濾過工程に替わる濁質成分の除濁方法として精密
濾過膜（以下、ＭＦ膜という）または限外濾過膜（以
下、ＵＦ膜という）等の膜濾過による浄水製造方法が注
目されている。2. Description of the Related Art Conventionally, as a method for producing water purification, a method has been established in which a coagulation settling step and a sand filtration step are combined and sterilization or chlorination is added thereto. However, since this method requires a large installation area, recently, a microfiltration membrane (hereinafter, referred to as an MF membrane) or an ultrafiltration membrane (hereinafter, referred to as an MF membrane) has been used as a method of removing turbid components instead of the coagulation sedimentation step and the sand filtration step. , UF membranes) have attracted attention.
【０００３】この膜濾過による浄水製造方法は、設置面
積が従来の数分の一にまでコンパクト化でき、広い設置
面積を確保しにくい都市部での浄水製造方法として適し
ている。膜濾過の方式にはクロスフロー濾過と全量濾過
があり、クロスフロー濾過の方が膜性能は長く維持でき
るが、いずれにしても濾過を継続しているうちに膜の目
詰まりが発生するので、膜を定期的に洗浄する必要があ
る。[0003] This method for producing purified water by membrane filtration is suitable as a method for producing purified water in an urban area where the installation area can be reduced to a fraction of the conventional size and it is difficult to secure a large installation area. There are two types of membrane filtration: cross-flow filtration and total filtration.Cross-flow filtration can maintain the membrane performance longer, but in any case, clogging of the membrane occurs while filtration is continued. The membrane needs to be cleaned regularly.
【０００４】[0004]
【発明が解決しようとする課題】しかしながら、膜濾過
による従来の浄水製造方法は、定期的な洗浄を行っても
膜の透過性が次第に低下し、膜性能を長期的に安定させ
ることができないという欠点がある。また、膜を洗浄し
た際に発生する大量の洗浄排水の処分についても問題が
あった。However, in the conventional method for producing water purification by membrane filtration, the permeability of the membrane gradually decreases even after regular cleaning, and the membrane performance cannot be stabilized for a long time. There are drawbacks. There is also a problem with disposal of a large amount of washing wastewater generated when the membrane is washed.
【０００５】本発明はこのような事情に鑑みてなされた
もので、膜性能を長期的に安定して維持することがで
き、且つ膜の洗浄排水量を低減できる浄水製造方法を提
案することを目的とする。[0005] The present invention has been made in view of such circumstances, and an object of the present invention is to propose a purified water production method capable of maintaining the membrane performance stably for a long period of time and reducing the amount of washing and drainage of the membrane. And
【０００６】[0006]
【課題を解決する為の手段】本発明は、前記目的を達成
する為に、精密濾過膜または限外濾過膜等の膜を用いて
汚水を膜濾過することにより浄水を製造すると共に、所
定の濾過時間ごとに洗浄機構により前記膜を洗浄する浄
水製造方法に於いて、前記汚水中の有機物濃度と濁度を
検出し、検出した有機物濃度と濁度との比の大小に応じ
て膜の洗浄時間と濾過時間のうち少なくとも一方を制御
することを特徴とする。SUMMARY OF THE INVENTION In order to achieve the above object, the present invention provides a method for producing purified water by subjecting wastewater to membrane filtration using a membrane such as a microfiltration membrane or an ultrafiltration membrane. In a water purification method in which the membrane is washed by a washing mechanism at each filtration time, an organic matter concentration and turbidity in the sewage are detected, and the membrane is washed in accordance with the ratio of the detected organic matter concentration to turbidity. At least one of the time and the filtration time is controlled.
【０００７】[0007]
【作用】本発明は、汚水中に含まれる有機物が膜に付着
すると、付着強度が大きく剥離しにくい性質があり、逆
に、濁度の主成分である無機物は付着強度が小さく、比
較的剥離し易い性質があるという知見に基づいて成され
たものである。本発明によれば、汚水を膜濾過する際
に、汚水中の有機物濃度と濁度を検出し、検出した有機
物濃度と濁度との比の大小に応じて膜の洗浄時間と濾過
時間のうち少なくとも一方を制御するようにした。即
ち、汚水中の有機物濃度に対して濁度の主成分である無
機物の比率が小さい場合、濾過時間を短くして早めに洗
浄したり、洗浄時間を長くしたりする。逆に、有機物濃
度に対して無機物の比率が大きい場合には、濾過時間を
長くしたり、洗浄時間を短くしたりする。According to the present invention, when organic matter contained in sewage adheres to a membrane, the adhesive strength is large and it is difficult to peel off. On the contrary, the inorganic substance which is the main component of turbidity has a small adhesive strength and is relatively peeled. This is based on the finding that there is an easy property. According to the present invention, when membrane filtration of sewage, the organic matter concentration and turbidity in the sewage are detected, and the membrane washing time and the filtration time are determined according to the ratio of the detected organic matter concentration to turbidity. At least one is controlled. That is, when the ratio of the inorganic substance, which is the main component of turbidity, to the organic substance concentration in the wastewater is small, the filtration time is shortened to perform the washing earlier, or the washing time is lengthened. Conversely, when the ratio of the inorganic substance to the organic substance concentration is large, the filtration time is lengthened or the cleaning time is shortened.
【０００８】また、本発明によれば、汚水を膜濾過する
際に、汚水中の有機物濃度を検出し、検出した有機物濃
度の大小に応じて膜の洗浄時間と濾過時間のうち少なく
とも一方を制御するようにした。即ち、汚水中の有機物
濃度が大きい場合には、濾過時間を短くして早めに洗浄
したり、洗浄時間を長くしたりする。逆に、有機物濃度
が小さい場合には、濾過時間を長くしたり、洗浄時間を
短くしたりする。Further, according to the present invention, when the sewage is subjected to membrane filtration, the concentration of organic matter in the sewage is detected, and at least one of the membrane washing time and the filtration time is controlled according to the detected concentration of the organic matter. I did it. That is, when the organic matter concentration in the sewage is large, the filtration time is shortened to perform the washing earlier, or the washing time is lengthened. Conversely, when the organic matter concentration is low, the filtration time is lengthened or the washing time is shortened.
【０００９】また、洗浄機構により発生する洗浄排水を
回転平膜モジュールにより固液分離するようにしたの
で、洗浄排水の大部分を浄水として回収することができ
る。Further, since the washing wastewater generated by the washing mechanism is separated into solid and liquid by the rotary flat membrane module, most of the washing wastewater can be recovered as purified water.
【００１０】[0010]
【実施例】以下添付図面に従って本発明に係る浄水製造
方法の好ましい実施例について詳説する。図１は、本発
明の浄水製造方法を適用する浄水製造設備の全体構成図
である。図１に示すように、原水配管１０は、有機物濃
度を検出する有機物濃度計１２、濁度を検出する濁度計
１４及びラインミキサー１６を介して原水貯留槽１８に
接続される。そして、原水配管１０を流れる被処理原水
は、塩素ライン２２から塩素が添加された後、有機物濃
度計１２により有機物濃度が検出されると共に、濁度計
１４により濁度が検出されコントローラ２４に逐次出力
される。また、被処理原水は、ラインミキサー１６の手
前で凝集剤ライン２６から凝集剤が添加され、ラインミ
キサー１６で凝集剤及び塩素と混合されて原水貯留槽１
８に流入する。このラインミキサー１６は、充分な混合
を行えるように４段以上の段数を有することが好まし
い。また、原水貯留槽１８では、後記する中空糸膜モジ
ュール２８の膜の目詰まりを促進する微細な濁質が凝集
剤により粗大化される。この場合、凝集剤の種類として
はポリ塩化アルミニウムが好ましく、濁質の粗大化を充
分行うために凝集剤の添加量を、Ａｌ2 Ｏ 3として０．
５ｍｇ／被処理原水ｌが好ましい。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of the water purification method according to the present invention will be described below in detail with reference to the accompanying drawings. FIG. 1 is an overall configuration diagram of a purified water production facility to which the purified water production method of the present invention is applied. As shown in FIG. 1, the raw water pipe 10 is connected to a raw water storage tank 18 via an organic matter concentration meter 12 for detecting an organic matter concentration, a turbidity meter 14 for detecting turbidity, and a line mixer 16. After chlorine is added from the chlorine line 22 to the raw water to be treated flowing through the raw water pipe 10, the organic matter concentration is detected by the organic matter concentration meter 12, the turbidity is detected by the turbidity meter 14, and the turbidity is sequentially detected by the controller 24. Is output. The raw water to be treated is added with a flocculant from a flocculant line 26 before the line mixer 16, mixed with the flocculant and chlorine in the line mixer 16 and mixed with the raw water storage tank 1.
Flow into 8. The line mixer 16 preferably has four or more stages so that sufficient mixing can be performed. In the raw water storage tank 18, fine turbidity that promotes clogging of the membrane of the hollow fiber membrane module 28 described later is coarsened by the coagulant. In this case, the type of the coagulant is preferably polyaluminum chloride, and the amount of the coagulant added is 0.1 as Al 2 O 3 in order to sufficiently increase the turbidity.
5 mg / l of raw water to be treated is preferred.
【００１１】また、原水貯留槽１８の底部から延びた供
給配管３０は、コントローラ２４からの指示により作動
・停止する供給ポンプ３２を介して中空糸膜モジュール
２８に接続される。この中空糸膜モジュール２８の膜素
材は、ポリプロピレン、ポリアクリロニトリル、ポリス
ルホン等の高分子材料やアルミナ等の無機材料を選択す
ることができるが、外圧中空糸膜が好ましい。A supply pipe 30 extending from the bottom of the raw water storage tank 18 is connected to a hollow fiber membrane module 28 via a supply pump 32 which is operated and stopped according to an instruction from a controller 24. The membrane material of the hollow fiber membrane module 28 can be selected from a polymer material such as polypropylene, polyacrylonitrile, and polysulfone, and an inorganic material such as alumina, but an external pressure hollow fiber membrane is preferable.
【００１２】また、中空糸膜モジュール２８の透過水側
から延びた透過水配管３４は処理水貯留槽３６に接続さ
れると共に、中空糸膜モジュール２８の濃縮水側から延
びた濃縮水配管３８は途中から分岐し、一方は洗浄用自
動弁４０を介して回転平膜モジュール４２に至るライン
を形成し、他方は戻り用自動弁４４を介して原水貯留槽
１８に戻るラインを形成する。また、濃縮水配管３８の
戻り用自動弁４４側には圧力計４６が設けられ、検出さ
れた圧力がコントローラ２４に逐次出力されることによ
り、中空糸膜モジュール２８の濾過圧力が把握される。
これにより、洗浄用自動弁４０を閉、戻り用自動弁４４
を開にした状態で供給ポンプ３２を作動させると、被処
理原水が中空糸膜モジュール２８で膜濾過される膜濾過
ラインを形成する。A permeated water pipe 34 extending from the permeated water side of the hollow fiber membrane module 28 is connected to a treated water storage tank 36, and a concentrated water pipe 38 extending from the concentrated water side of the hollow fiber membrane module 28 is Branching from the middle, one forms a line to the rotating flat membrane module 42 via the automatic cleaning valve 40, and the other forms a line returning to the raw water storage tank 18 via the automatic return valve 44. A pressure gauge 46 is provided on the return pipe 44 side of the concentrated water pipe 38, and the detected pressure is sequentially output to the controller 24, so that the filtration pressure of the hollow fiber membrane module 28 can be grasped.
As a result, the automatic cleaning valve 40 is closed, and the automatic return valve 44 is closed.
When the supply pump 32 is operated in the state in which is opened, a membrane filtration line is formed in which raw water to be treated is subjected to membrane filtration by the hollow fiber membrane module 28.
【００１３】また、回転平膜モジュール２８から延びた
分離水配管４８は透過水配管３４に合流されると共に、
回転平膜モジュール２８から延びた汚泥排出配管５０
は、コントローラ２４からの指示で開閉する汚泥排出バ
ルブ５２を介して図示しない汚泥処理設備に送られる。
また、処理水貯留槽３６から延びた洗浄用配管５４は、
コントローラ２４からの指示で作動・停止する洗浄用ポ
ンプ５６を介して中空糸膜モジュール２８の透過水側に
接続される。これにより、戻り用自動弁４４を閉、洗浄
用自動弁４０を開にした状態で、供給ポンプ３２を停止
して洗浄用ポンプ５６を作動させると、処理水貯留槽３
６に貯留された透過水が中空糸膜モジュール２８を逆洗
して回転平膜モジュール４２に至る逆圧水洗ラインを形
成する。The separation water pipe 48 extending from the rotary flat membrane module 28 is joined to the permeated water pipe 34,
Sludge discharge pipe 50 extending from rotary flat membrane module 28
Is sent to a sludge treatment facility (not shown) via a sludge discharge valve 52 that opens and closes according to an instruction from the controller 24.
The cleaning pipe 54 extending from the treated water storage tank 36 is
It is connected to the permeated water side of the hollow fiber membrane module 28 via a cleaning pump 56 that is activated and stopped according to an instruction from the controller 24. Thus, when the supply pump 32 is stopped and the cleaning pump 56 is operated in a state where the automatic return valve 44 is closed and the automatic cleaning valve 40 is opened, the treated water storage tank 3
The permeated water stored in 6 backwashes the hollow fiber membrane module 28 to form a back pressure washing line leading to the rotary flat membrane module 42.
【００１４】また、中空糸膜モジュール２８にはエア配
管５８が配設され、コントローラ２４からの指示で開閉
するエア用自動弁６０を介してコンプレッサー６２接続
される。これにより、エア用自動弁６０が開くと、コン
プレッサー６２からの加圧エアが中空糸膜モジュール２
８内に吹き込まれ、中空糸膜の内側から外側に流れて中
空糸膜を膨張させながら中空糸膜を空気スクラビング洗
浄するエア洗浄ラインを形成する。An air pipe 58 is provided in the hollow fiber membrane module 28, and is connected to a compressor 62 via an automatic air valve 60 which opens and closes according to an instruction from the controller 24. Thereby, when the air automatic valve 60 is opened, the pressurized air from the compressor 62 is supplied to the hollow fiber membrane module 2.
The air washing line is blown into the inside 8 and flows from the inside to the outside of the hollow fiber membrane to expand the hollow fiber membrane and perform air scrubbing and cleaning of the hollow fiber membrane.
【００１５】次に、上記の如く構成された浄水製造設備
を用いて本発明の浄水製造方法を説明する。濁質及び有
機物等の汚濁物質を含む被処理原水は、凝集剤が添加さ
れて微細な濁質が粗大化されたのち、中空糸膜モジュー
ル２８で膜濾過されて透過水と濃縮水に分離される。こ
の分離操作を続けると、中空糸膜の膜面に濁質及び有機
物等の汚濁物質による付着層が形成されてきて、被処理
原水の透過水量が低下する。そして、本発明の発明者
は、付着層の付着強度は、付着層を構成する濁質成分
（濁度に影響し、主に二酸化珪素、酸化アルミニウム等
の無機成分で構成される）の量と、有機物の量とにより
異なるという知見を得た。即ち、有機物は膜に付着する
と剥離しにくい性質があり、濁質の主成分である無機物
は膜に付着しても比較的剥離し易い性質がある。Next, the water purification method of the present invention will be described using the water purification equipment configured as described above. Raw water to be treated containing pollutants such as turbid substances and organic substances is subjected to membrane filtration in the hollow fiber membrane module 28 after separation of fine turbid substances by adding a flocculant, and separated into permeated water and concentrated water. You. If this separation operation is continued, an adhered layer of pollutants such as turbid substances and organic substances is formed on the membrane surface of the hollow fiber membrane, and the amount of permeated water to be treated decreases. The inventor of the present invention has found that the adhesion strength of the adhesion layer depends on the amount of the turbid component (which affects the turbidity and is mainly composed of inorganic components such as silicon dioxide and aluminum oxide) constituting the adhesion layer. And the fact that it differs depending on the amount of organic matter. That is, an organic substance has a property that it is hard to peel off when it adheres to a film, and an inorganic substance that is a main component of a turbid substance has a property that it relatively easily peels off even if it adheres to a film.
【００１６】そこで、本発明の浄水製造方法では、被処
理原水の濁度を検出すると共に、有機物濃度を検出し、
この検出した濁度と有機物濃度の比（濁度／有機物濃
度）の大小に応じて膜の洗浄時間と濾過時間の少なくと
も一方を制御するようにしたもので、濁度の評価に光電
比色計を使用し、有機物濃度の評価にＵＶモニタを使用
した例で以下に説明する。尚、ＵＶモニタ（紫外線吸収
モニタ）で評価される有機物濃度は、２６０ｎｍの波長
における被処理原水の吸光度Ｅを１００倍して表した。Therefore, in the method for producing purified water of the present invention, the turbidity of the raw water to be treated is detected, and the concentration of the organic matter is detected.
At least one of the membrane washing time and the filtration time is controlled according to the magnitude of the ratio of the detected turbidity to the organic substance concentration (turbidity / organic substance concentration). And an example in which a UV monitor is used to evaluate the organic substance concentration will be described below. The organic substance concentration evaluated by a UV monitor (ultraviolet absorption monitor) was represented by multiplying the absorbance E of the raw water to be treated at a wavelength of 260 nm by 100.
【００１７】そして、濁度／有機物濃度が０．５〜１．
０の範囲にある時は、中空糸膜の表面に形成される付着
層の付着強度は中ぐらいである。この場合は、中空糸膜
モジュール２８の濾過圧力を検出する圧力計４６が所定
値になったところで前記した膜濾過ラインの運転を停止
し、先ず前記したエア洗浄ラインの運転を行って中空糸
膜を６０秒間空気スクラビング洗浄し、引き続き前記し
た逆圧水洗ラインの運転を行って中空糸膜を５秒間逆圧
水洗する。The turbidity / organic substance concentration is 0.5-1.
When it is in the range of 0, the adhesion strength of the adhesion layer formed on the surface of the hollow fiber membrane is moderate. In this case, when the pressure gauge 46 for detecting the filtration pressure of the hollow fiber membrane module 28 reaches a predetermined value, the operation of the above-mentioned membrane filtration line is stopped, and the operation of the above-mentioned air washing line is performed first to perform the hollow fiber membrane filtration. Is cleaned by air scrubbing for 60 seconds, and then the above-described operation of the back pressure water washing line is performed to backwash the hollow fiber membrane with the back pressure water for 5 seconds.
【００１８】また、濁度／有機物濃度が０．５以下の
時、即ち有機物濃度が高い時は、付着層の付着強度は大
きく、中空糸膜の表面はベタつくようになる。この場合
は、中空糸膜モジュール２８の濾過圧力が所定値になっ
たところで、膜濾過ラインの運転を停止し、先ずエア洗
浄ラインの運転を行って中空糸膜を１２０秒間空気スク
ラビング洗浄し、引き続き逆圧水洗ラインの運転を行っ
て中空糸膜を５秒間逆圧水洗する。When the turbidity / organic substance concentration is 0.5 or less, that is, when the organic substance concentration is high, the adhesion strength of the adhesion layer is large and the surface of the hollow fiber membrane becomes sticky. In this case, when the filtration pressure of the hollow fiber membrane module 28 reaches a predetermined value, the operation of the membrane filtration line is stopped, the air cleaning line is first operated, and the hollow fiber membrane is scrubbed with air for 120 seconds. The hollow fiber membrane is backwashed for 5 seconds by operating the backwashing line.
【００１９】また、濁度／有機物濃度が１．０以上の
時、即ち無機物濃度が高い時は、付着層の付着強度は小
さくなる。この場合は、中空糸膜モジュール２８の濾過
圧力が所定値になったところで、膜濾過ラインの運転を
停止し、先ずエア洗浄ラインの運転を行って中空糸膜を
３０秒間空気スクラビング洗浄し、逆圧水洗ラインの運
転は行わない。When the turbidity / organic substance concentration is 1.0 or more, that is, when the inorganic substance concentration is high, the adhesion strength of the adhesion layer becomes small. In this case, when the filtration pressure of the hollow fiber membrane module 28 reaches a predetermined value, the operation of the membrane filtration line is stopped, and the air cleaning line is first operated to perform air scrubbing and cleaning of the hollow fiber membrane for 30 seconds. No operation of the pressure washing line is performed.
【００２０】また、上記した濁度／有機物濃度による洗
浄時間の設定とは別に、濁度が２０度を越える場合に
は、中空糸膜モジュール２８内の濁質量が増大すること
により、中空糸膜の間隙に濁質が滞留するインターファ
イバークロッキング現象を生じ易い。この場合は、前記
空気スクラビング洗浄及び逆圧水洗の他に、濾過時間を
短くして中空糸膜モジュール２８内の濁質量が許容濁質
濃度以下、例えば１０００度以下になるようにする。更
に、逆圧水洗で発生する洗浄排水を固液分離する回転平
膜モジュール４２内の汚泥濃度が限界値を越えないよう
に、汚泥排出バルブ５２の開時間を長くとるようにす
る。一般的に回転平膜モジュール４２内の汚泥濃度は７
〜１０％程度が適当である。In addition to the above-mentioned setting of the washing time based on the turbidity / organic substance concentration, when the turbidity exceeds 20 degrees, the turbid mass in the hollow fiber membrane module 28 increases, and the hollow fiber membrane is increased. The interfiber clocking phenomenon in which the turbid matter stays in the gaps of the liquid crystal tends to occur. In this case, besides the air scrubbing washing and the back pressure washing, the filtration time is shortened so that the turbid mass in the hollow fiber membrane module 28 is less than the allowable turbid concentration, for example, 1000 degrees or less. Further, the opening time of the sludge discharge valve 52 is set to be long so that the sludge concentration in the rotary flat membrane module 42 for solid-liquid separation of the washing waste water generated by the back pressure washing does not exceed a limit value. Generally, the sludge concentration in the rotating flat membrane module 42 is 7
About 10% is appropriate.
【００２１】また、逆圧水洗により発生した洗浄排水
は、回転平膜モジュール４２で固液分離され、固液分離
された分離水は分離水配管４８を通って処理水として透
過水配管３４に合流する。これにより、処理水の回収率
（被処理原水の使用量に対する処理水の発生量）を高く
することができる。例えば、濁度が１０度の被処理原水
を１０００ｍ3 ／ｄａｙ処理した時、１０％の濃縮液と
して１００ｌ／ｄａｙ排出すればよく、処理水の回収率
としては９９．９９％となり、極めて効率のよい処理を
行うことができる。The washing waste water generated by the back pressure water washing is separated into solid and liquid by the rotary flat membrane module 42, and the separated water is separated into the permeated water pipe 34 as the treated water through the separated water pipe 48. I do. This makes it possible to increase the recovery rate of the treated water (the amount of the treated water generated with respect to the used amount of the raw water to be treated). For example, when raw water having a turbidity of 10 degrees is subjected to 1000 m 3 / day treatment, 100 l / day may be discharged as a 10% concentrated liquid, and the recovery rate of the treated water is 99.99%, which is extremely efficient. Good processing can be performed.
【００２２】尚、本実施例では、濁度と有機物濃度の比
（濁度／有機物濃度）の大小に応じ洗浄時間を制御する
ことで説明したが、濁度／有機物濃度に応じて洗浄から
次の洗浄までの間の濾過時間を制御するようにしてもよ
い。また、被処理原水の有機物濃度だけを検出して、こ
の有機物濃度の大小に応じて濾過時間と洗浄時間の少な
くとも一方を制御するようにしてもよい。In this embodiment, the explanation was made by controlling the cleaning time in accordance with the ratio of the turbidity to the organic substance concentration (turbidity / organic substance concentration). The filtration time until the washing of may be controlled. Alternatively, only the concentration of the organic substance in the raw water to be treated may be detected, and at least one of the filtration time and the washing time may be controlled according to the level of the organic substance.
【００２３】[0023]
【発明の効果】以上説明したように、本発明によれば、
汚水中の有機物濃度と濁度を検出し、検出した有機物濃
度と濁度との比の大小に応じて濾過時間と膜の洗浄時間
のうち少なくとも一方を制御するようにした。本発明に
係る浄水製造方法によれば、汚水中の有機物濃度を検出
し、検出した有機物濃度の大小に応じて濾過時間と膜の
洗浄時間のうち少なくとも一方を制御するようにした。As described above, according to the present invention,
The organic matter concentration and turbidity in the sewage were detected, and at least one of the filtration time and the membrane washing time was controlled according to the magnitude of the ratio between the detected organic matter concentration and turbidity. According to the method for producing purified water according to the present invention, the concentration of the organic matter in the sewage is detected, and at least one of the filtration time and the membrane cleaning time is controlled according to the magnitude of the detected organic matter concentration.
【００２４】これにより、膜に付着する付着物の付着強
度に応じて、膜の洗浄時間と濾過時の少なくとも一方を
適切に制御することができるので、長期間安定した膜性
能を維持することができる。また、洗浄機構により発生
する洗浄排水を回転平膜モジュールにより固液分離し、
洗浄排水の大部分を浄水として回収するようにしたの
で、洗浄排水の発生量を少なくすることができ、汚水処
理量に対する浄水の回収率を向上させることができる。[0024] According to this, at least one of the membrane washing time and the filtration time can be appropriately controlled according to the adhesion strength of the deposits adhering to the membrane, so that stable membrane performance can be maintained for a long period of time. it can. In addition, the washing wastewater generated by the washing mechanism is separated into solid and liquid by a rotating flat membrane module,
Since most of the cleaning wastewater is collected as purified water, the generation amount of the cleaning wastewater can be reduced, and the recovery rate of the purified water with respect to the wastewater treatment amount can be improved.
【図１】図１は、本発明に係る浄水製造方法を適用する
浄水製造設備の全体構成図FIG. 1 is an overall configuration diagram of a purified water production facility to which a purified water production method according to the present invention is applied.
１２…有機物濃度計 １４…濁度計 １６…ラインミキサー １８…原水貯留槽 ２４…コントローラ ２８…中空糸膜モジュール ３２…供給ポンプ ４０…洗浄用自動弁 ４２…回転平膜モジュール ４４…戻り用自動弁 ４６…圧力計 ５２…汚泥排出バルブ ６０…エア用自動弁 ６２…コンプレッサー 12 Organic Concentration Meter 14 Turbidity Meter 16 Line Mixer 18 Raw Water Storage Tank 24 Controller 28 Hollow Fiber Membrane Module 32 Supply Pump 40 Automatic Cleaning Valve 42 Rotating Flat Membrane Module 44 Automatic Return Valve 46 ... Pressure gauge 52 ... Sludge discharge valve 60 ... Automatic valve for air 62 ... Compressor
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平５−317660（ＪＰ，Ａ) 特開 平７−204475（ＪＰ，Ａ) 特開 平６−238136（ＪＰ，Ａ) (58)調査した分野(Int.Cl.6，ＤＢ名) B01D 65/02 B01D 61/22 C02F 1/44 ────────────────────────────────────────────────── ─── Continuation of the front page (56) References JP-A-5-317660 (JP, A) JP-A-7-204475 (JP, A) JP-A-6-238136 (JP, A) (58) Field (Int.Cl. 6 , DB name) B01D 65/02 B01D 61/22 C02F 1/44
Claims (3)
て汚水を膜濾過することにより浄水を製造すると共に、
所定の濾過時間ごとに洗浄機構により前記膜を洗浄する
浄水製造方法に於いて、 前記汚水中の有機物濃度と濁度を検出し、検出した有機
物濃度と濁度との比の大小に応じて膜の洗浄時間と濾過
時間のうち少なくとも一方を制御することを特徴とする
浄水製造方法。1. Purified water is produced by subjecting sewage to membrane filtration using a membrane such as a microfiltration membrane or an ultrafiltration membrane.
In a water purification method for washing the membrane by a washing mechanism every predetermined filtration time, the organic matter concentration and turbidity in the sewage are detected, and the membrane is determined according to the ratio of the detected organic matter concentration to turbidity. A method for controlling at least one of a washing time and a filtration time.
て汚水を膜濾過することにより浄水を製造すると共に、
所定の濾過時間ごとに洗浄機構により前記膜を洗浄する
浄水製造方法に於いて、 前記汚水中の有機物濃度を検出し、検出した有機物濃度
の大小に応じて膜の洗浄時間と濾過時間のうち少なくと
も一方を制御することを特徴とする浄水製造方法。2. Purified water is produced by subjecting waste water to membrane filtration using a membrane such as a microfiltration membrane or an ultrafiltration membrane.
In the purified water manufacturing method of washing the membrane by a washing mechanism every predetermined filtration time, detecting an organic matter concentration in the sewage, at least one of the membrane washing time and the filtration time according to the detected organic matter concentration. A method for producing purified water, characterized in that one is controlled.
膜モジュールにより固液分離することを特徴とする請求
項１または２の浄水製造方法。3. The method for producing purified water according to claim 1, wherein the washing wastewater generated in the washing mechanism is separated into solid and liquid by a rotating flat membrane module.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3099694A JP2876978B2 (en) | 1994-02-02 | 1994-02-02 | Water purification method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3099694A JP2876978B2 (en) | 1994-02-02 | 1994-02-02 | Water purification method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07213875A JPH07213875A (en) | 1995-08-15 |
| JP2876978B2 true JP2876978B2 (en) | 1999-03-31 |
Family
ID=12319215
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3099694A Expired - Fee Related JP2876978B2 (en) | 1994-02-02 | 1994-02-02 | Water purification method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2876978B2 (en) |
Families Citing this family (16)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP3381556B2 (en) * | 1997-06-05 | 2003-03-04 | 日立プラント建設株式会社 | Water purification method and device |
| KR100233308B1 (en) * | 1997-07-04 | 1999-12-01 | 신형인 | Purification method by hollow fiber membrane |
| JP4058867B2 (en) * | 1999-11-10 | 2008-03-12 | 株式会社日立プラントテクノロジー | Water purification system and method |
| JP2002035554A (en) * | 2000-07-24 | 2002-02-05 | Nkk Corp | Method for treating water and its apparatus |
| FR2817768B1 (en) * | 2000-12-13 | 2003-08-29 | Lyonnaise Eaux Eclairage | METHOD FOR REGULATING A MEMBRANE FILTRATION SYSTEM |
| JP2003053155A (en) * | 2001-08-13 | 2003-02-25 | Asahi Kasei Corp | Membrane filtration method |
| US6821428B1 (en) * | 2002-03-28 | 2004-11-23 | Nalco Company | Method of monitoring membrane separation processes |
| JP4569200B2 (en) * | 2004-07-23 | 2010-10-27 | 富士電機ホールディングス株式会社 | Water treatment method and membrane filtration water treatment device operation method |
| JP5054289B2 (en) * | 2005-05-25 | 2012-10-24 | Ｊｆｅエンジニアリング株式会社 | Operation method of membrane separator |
| JP2006326472A (en) * | 2005-05-25 | 2006-12-07 | Jfe Engineering Kk | Membrane separation apparatus |
| JP2006326471A (en) * | 2005-05-25 | 2006-12-07 | Jfe Engineering Kk | Membrane separation apparatus and its operation method |
| JP5103747B2 (en) * | 2006-02-03 | 2012-12-19 | 栗田工業株式会社 | Water treatment apparatus and water treatment method |
| JP2007245049A (en) * | 2006-03-17 | 2007-09-27 | Fuji Electric Holdings Co Ltd | Water treatment process |
| JP5277519B2 (en) * | 2006-05-17 | 2013-08-28 | 富士電機株式会社 | Water treatment method |
| JP5589481B2 (en) * | 2010-03-25 | 2014-09-17 | 三浦工業株式会社 | Filtration system |
| JP6812198B2 (en) * | 2016-10-21 | 2021-01-13 | 株式会社日立製作所 | Water treatment equipment and water treatment method |
-
1994
- 1994-02-02 JP JP3099694A patent/JP2876978B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH07213875A (en) | 1995-08-15 |
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