JP2724673B2 - Surface water purification method and device therefor - Google Patents
Surface water purification method and device thereforInfo
- Publication number
- JP2724673B2 JP2724673B2 JP6027444A JP2744494A JP2724673B2 JP 2724673 B2 JP2724673 B2 JP 2724673B2 JP 6027444 A JP6027444 A JP 6027444A JP 2744494 A JP2744494 A JP 2744494A JP 2724673 B2 JP2724673 B2 JP 2724673B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- membrane module
- backwashing
- path
- filtration membrane
- 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 - Lifetime
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- Separation Using Semi-Permeable Membranes (AREA)
Description
【０００１】[0001]
【産業上の利用分野】本発明は、河川水や湖沼水等の表
流水の腰浄化方法及びその装置に関するものであり、特
に限外または精密瀘過膜モジュールを利用した表流水の
膜浄化方法およびその装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for purifying surface water such as river water and lake water, and more particularly to a method for purifying surface water using an ultra or precision filtration membrane module.
The present invention relates to a membrane purification method and an apparatus therefor.
【０００２】[0002]
【従来の技術】従来、河川水や湖沼水等の表流水から水
道水を得るための浄水処理システムとしては、凝集−沈
澱−砂濾過−塩素滅菌工程を経るのが一般的である。こ
のような工程を実現するためには、凝集池、沈澱池、砂
濾過池、塩素滅菌設備が必要であり、大きな設置スペー
スを要するという問題点がある。加えて、近年河川等の
水源の汚濁が進んでいるため、これに対する新しい高度
浄水処理システムの開発が求められ、上記工程に活性炭
処理システムやオゾン処理システムを付加することが提
案されている。2. Description of the Related Art Conventionally, a water purification system for obtaining tap water from surface water such as river water or lake water generally involves a coagulation-precipitation-sand filtration-chlorine sterilization process. In order to realize such a process, a coagulation pond, a sedimentation pond, a sand filtration pond, and a chlorine sterilization facility are required, and there is a problem that a large installation space is required. In addition, since the pollution of water sources such as rivers has been increasing in recent years, development of a new advanced water purification treatment system has been required, and it has been proposed to add an activated carbon treatment system or an ozone treatment system to the above process.
【０００３】しかしながら、従来の浄水処理システムに
上述した活性炭処理システムやオゾン処理システムを付
加することは、設置スペースの更なる増加を招き、複雑
な計測制御技術をも必要とする新たな問題点が生ずる。However, the addition of the above-mentioned activated carbon treatment system and ozone treatment system to the conventional water purification treatment system causes a further increase in installation space and a new problem requiring complicated measurement control technology. Occurs.
【０００４】これに対し、限外または精密濾過膜と呼ば
れる新しい材料の利用技術が多方面にわたって提案され
ており、その一例として中空糸型限外または精密濾過膜
モジュールを使用した浄水処理システムの実用化が検討
されている。[0004] On the other hand, techniques for using a new material called an ultrafiltration or microfiltration membrane have been proposed in various fields, and as an example, the practical use of a water purification system using a hollow fiber type ultrafiltration or microfiltration membrane module has been proposed. Is being considered.
【０００５】その一例を図３を参照して説明する。図３
において、逆止弁２０を経て導入された河川水等の原水
は、ポンプ２１により昇圧されて中空糸型限外濾過膜モ
ジュール（以下、ＵＦモジュールと呼ぶことがある）２
２に供給される。ＵＦモジュール２２は、簡単に言え
ば、中空糸状の限外濾過膜を多数集合させたものであ
り、この中空糸膜の内側に濁質成分を含む原水を供給す
ると、濁質成分を除去された透過水が中空糸膜外に得ら
れる。このようにして、ＵＦモジュール２２では、限外
濾過膜の濾過作用により濁質成分を除去した透過水を、
透過水自動弁２３を通して次段の処理施設に供給する。An example will be described with reference to FIG. FIG.
, Raw water such as river water introduced through a check valve 20 is pressurized by a pump 21 and is supplied with a hollow fiber ultrafiltration membrane module (hereinafter sometimes referred to as a UF module) 2.
2 is supplied. The UF module 22 is simply a collection of a number of hollow fiber ultrafiltration membranes. When raw water containing a turbid component is supplied inside the hollow fiber membrane, the turbid component is removed. Permeate is obtained outside the hollow fiber membrane. Thus, in the UF module 22, the permeated water from which the turbid components have been removed by the filtration action of the ultrafiltration membrane is
The water is supplied to the next treatment facility through the automatic permeated water valve 23.
【０００６】ところで、ＵＦモジュール２２内では中空
糸膜の内側表面に透過されない濁質成分が蓄積し、詰ま
って処理能力の低下、ひいては運転停止の原因となるの
で、これを排出する処理が必要である。これは、ＵＦモ
ジュール２２の中空糸膜に供給する水流を高速とするこ
とで実現されている。すなわち、中空糸膜の内表面に糸
の長さ方向と平行に高速の水流（クロスフロー）を与え
ることで中空糸膜の内表面に付着している濁質成分を、
いわばはぎとるものである。Meanwhile, in the UF module 22, turbid components that are not permeated accumulate on the inner surface of the hollow fiber membrane and are clogged, resulting in a reduction in processing capacity and, consequently, an operation stoppage. is there. This is realized by increasing the speed of the water flow supplied to the hollow fiber membrane of the UF module 22. That is, by giving a high-speed water flow (cross flow) to the inner surface of the hollow fiber membrane in parallel with the length direction of the yarn, the turbid component adhering to the inner surface of the hollow fiber membrane is removed.
In a sense, it's stripped.
【０００７】このため、ＵＦモジュール２２内における
中空糸膜の内側に連通する出口には、濁質成分を大量に
含んだ濃縮水を濃縮水排出自動弁２４を通してその一部
を常時排出する経路２５と、高速の水流を得るためにＵ
Ｆモジュール２２に供給された原水をポンプ２１のサク
ション側に戻すための循環経路２６が接続される。ポン
プ２１のサクション側に戻される循環流量は、逆止弁２
０を経て供給される原水の流量に比べて通常１０倍程度
以上とはるかに多い。このようなＵＦモジュール２２か
らポンプ２１のサクション側に原水を戻す処理方式は、
クロスフロー方式と呼ばれる。For this reason, the outlet communicating with the inside of the hollow fiber membrane in the UF module 22 is provided with a path 25 for constantly discharging a part of the concentrated water containing a large amount of turbid components through the concentrated water discharge automatic valve 24. And to get high speed water flow
A circulation path 26 for returning the raw water supplied to the F module 22 to the suction side of the pump 21 is connected. The circulating flow returned to the suction side of the pump 21 depends on the check valve 2
The flow rate of raw water supplied through zero is usually about 10 times or more, which is much higher. The processing method of returning raw water from the UF module 22 to the suction side of the pump 21 is as follows.
This is called a cross flow method.
【０００８】前記のクロスフローのため、ポンプ２１の
容量は、同程度の処理能力を持つ従来の凝集−沈澱−砂
濾過による浄水処理システムにおけるポンプの容量に比
べてはるかに大きく、従って電力消費量も従来方式のポ
ンプの電力消費量に比べてはるかに多く、ランニングコ
ストが高くなるという問題点がある。加えて、濃縮水の
排出は連続して行われており、例えば原水の流入量を１
としたとき、透過水を０．３得る場合は、濃縮水の割合
は０．７となり、水の大部分を捨てていることになるの
で、回収率は３０％と悪いという問題点もある。なお、
ここでは透過水の流量をＰ、濃縮水の排出流量をＣとす
ると、回収率は１００×Ｐ／（Ｐ＋Ｃ）（％）で表され
る。Because of the cross flow described above, the capacity of the pump 21 is much greater than the capacity of the pump in a conventional flocculation-sedimentation-sand filtration water treatment system with comparable capacity, and thus the power consumption. Also, there is a problem that the power consumption is much higher than the power consumption of the conventional pump, and the running cost is increased. In addition, the discharge of concentrated water is performed continuously.
Then, when 0.3 permeated water is obtained, the ratio of the concentrated water is 0.7, and most of the water is discarded. Therefore, there is also a problem that the recovery rate is as poor as 30%. In addition,
Here, assuming that the flow rate of the permeated water is P and the discharge flow rate of the concentrated water is C, the recovery rate is expressed as 100 × P / (P + C) (%).
【０００９】[0009]
【発明が解決しようとする課題】これに対して本発明者
等は先に図４に示す表流水の膜浄化方法および膜浄化装
置の運転方法を提案した（特願平４−２１５４４３号、
特開平６−３１２７０と同じ）。図４において、逆止弁
３０、ポンプ３１、ＵＦモジュール３２、透過水自動弁
３３、洗浄水排出自動弁３４の構成に加えて、透過水を
蓄積するための透過水タンク３７、蓄積された透過水を
ＵＦモジュール３２の出口側に戻して逆洗を行うための
ポンプ３８、逆洗自動弁３９とを設けている。この処理
システムの通常運転に際しては、透過水自動弁３３を
開、洗浄水排出自動弁３４、逆洗自動弁３９は共に閉と
し、ポンプ３８を停止状態におく。このようにして、逆
止弁３０を経て導入された河川水等の原水は、ポンプ３
１により昇圧されてＵＦモジュール３２に供給される。
ＵＦモジュール３２では、限外濾過膜の濾過作用により
濁質成分を除去した透過水を、透過水自動弁３３を通し
て透過水タンク３７に蓄積する。なお、この通常運転の
間、循環経路３６を通して原水の流入量に対してゼロを
越え６倍以下程度の量のクロスフローが行われるが、透
過水量は原水量に等しい。逆洗は、例えば３０分ないし
１時間程度の定時間間隔で３０〜６０秒の間行われる。
この場合、原水の供給を停止すると共に透過水自動弁３
３を閉、洗浄水排出経路３５に設けた洗浄水排出自動弁
３４、逆洗自動弁３９は共に開とし、ポンプ３１を停止
状態でポンプ３８を運転する。このようにして、透過水
タンク３７に蓄積された透過水の一部を利用してＵＦモ
ジュール３２に対する逆洗が行われ、逆洗により中空糸
膜の内表面からはぎとられた濁質成分は、洗浄水ととも
に洗浄水排出自動弁３４を通してシステム外に排出され
る。これによると逆洗に消費される水量は洗浄水排出水
量に等しくなる。On the other hand, the present inventors have previously proposed a method for purifying surface water with a membrane and a method for operating a membrane purification apparatus shown in FIG. 4 (Japanese Patent Application No. 4-215443,
The same as in JP-A-6-31270). In FIG. 4, in addition to the check valve 30, the pump 31, the UF module 32, the automatic permeated water valve 33, and the automatic cleaning water discharge valve 34, a permeated water tank 37 for accumulating permeated water, A pump 38 and a backwash automatic valve 39 for returning water to the outlet side of the UF module 32 for backwashing are provided. During normal operation of this processing system, the automatic permeated water valve 33 is opened, the automatic cleaning water discharge valve 34 and the automatic backwash valve 39 are closed, and the pump 38 is stopped. Raw water such as river water introduced through the check valve 30 in this manner is supplied to the pump 3
1 and is supplied to the UF module 32.
In the UF module 32, the permeated water from which the turbid components have been removed by the filtration action of the ultrafiltration membrane is accumulated in the permeated water tank 37 through the permeated water automatic valve 33. During the normal operation, a cross flow of more than zero and about six times or less with respect to the inflow of raw water through the circulation path 36 is performed, but the amount of permeated water is equal to the amount of raw water. The backwashing is performed at regular time intervals of, for example, about 30 minutes to 1 hour for 30 to 60 seconds.
In this case, the supply of raw water is stopped and the automatic permeated water valve 3
3 is closed, the automatic cleaning water discharge valve 34 and the automatic backwash valve 39 provided in the cleaning water discharge path 35 are both opened, and the pump 38 is operated with the pump 31 stopped. In this way, the UF module 32 is backwashed using a part of the permeated water accumulated in the permeated water tank 37, and the turbid component stripped from the inner surface of the hollow fiber membrane by the backwash is The cleaning water is discharged out of the system together with the cleaning water through the cleaning water discharge automatic valve 34. According to this, the amount of water consumed for backwashing is equal to the amount of washwater discharge water.
【００１０】前記提案によれば限外または精密濾過膜モ
ジュールを利用した表流水の浄化処理システムにおい
て、全量濾過に近い回収率が得られ、またランニングコ
ストの低減化が図れることを明らかにした。According to the above proposal, it has been clarified that, in a purification system for surface water using an ultra- or microfiltration membrane module, a recovery rate close to full-volume filtration can be obtained and running costs can be reduced.
【００１１】しかし前記提案の浄化システムにおいて
は、中空糸型濾過膜モジュールの原水の入口付近に汚泥
（濁質成分）が貯まり易く、また逆洗時における中空糸
型濾過膜の原水側の水流方向は通常運転時と変わらず、
中空糸の長さがその径に比べて非常に長いこともあって
濁質成分の排出が必ずしも十分とはいえなかった。その
ため逆洗から通常運転に復帰した際、排出されずに残っ
た濁質成分が再び濾過膜に付着し、逆洗によって流量が
前の通常運転開始時のレベルまで戻りにくく、従ってこ
のような通常運転と逆洗を繰り返すにつれ流量が次第に
低下するという改善すべき点があった。However, in the proposed purification system, the sludge (turbid component) is likely to be stored near the inlet of the raw water of the hollow fiber type filtration membrane module, and the water flow direction on the raw water side of the hollow fiber type filtration membrane during backwashing. Is the same as during normal operation,
Since the length of the hollow fiber was much longer than its diameter, the discharge of the turbid component was not always sufficient. Therefore, when returning from the backwashing to the normal operation, the turbid components remaining without being discharged adhere to the filtration membrane again, and it is difficult for the backwashing to return the flow rate to the level at the time of the start of the previous normal operation. There was a point to be improved that the flow rate gradually decreased as the operation and backwashing were repeated.
【００１２】なお特開平４−２６０４２２号公報には、
フィルタ膜モジュールを用い、通常運転と逆洗とを繰り
返しながら原水を処理する方法および装置が提案されて
いるが、逆洗時にも常に原水を膜モジュールに供給し続
けるものであり、逆洗時の原水の損失が非常に大きいも
のである。Japanese Patent Application Laid-Open No. 4-260422 discloses that
A method and an apparatus for treating raw water while repeating normal operation and backwashing using a filter membrane module have been proposed.However, raw water is always supplied to the membrane module even at the time of backwashing. The loss of raw water is very large.
【００１３】[0013]
【課題を解決するための手段】本発明等は前記課題に対
し鋭意検討した結果、逆洗による濁質成分を含んだ洗浄
水の排出経路の取り付け箇所及び逆洗方法を工夫するこ
とにより解決出来るとの知見を得て、本発明を完成させ
ることが出来た。Means for Solving the Problems As a result of intensive studies on the above-mentioned problems, the present invention can be solved by devising an installation point of a discharge path of washing water containing a turbid component by back washing and a back washing method. Thus, the present invention was completed.
【００１４】すなわち本発明の第一は、中空糸型眼外ま
たは精密濾過膜モジュールを用いてクロスフロー全量濾
過により表流水を浄化する方法において、前記中空糸型
濾過膜モジュールを該濾過膜モジュールからの透過水ま
たは別途供給される清浄水により圧力制御またはあらか
じめ定められた周期で所定圧力範囲で間欠的な逆洗を行
うに際し、前記濾過膜モジュールに透過水出口経路を原
水側入口の近傍および非透過水出口の近傍の二箇所に設
け、洗浄水排出経路を前記濾過膜モジュールの原水供給
経路および非透過水のクロスフロー循環経路の二箇所に
分岐して設置し、各逆洗の度に前記二箇所に設けた透過
水の出口経路のうち、洗浄水の排出経路から遠い位置に
ある透過水の出口経路から逆洗のための洗浄水を交互に
供給し、前記分岐して設置された洗浄水排出経路より交
互に排出させることを特徴とする表流水の膜浄化方法、
または、前記間欠的逆洗を行いながらその間欠的に行わ
れる逆洗とは無関係に、透過水の採取を停止した状態
で、原水による濾過膜モジュールのフラッシングまたは
逆洗を伴う原水による濾過膜モジュールのフラッシング
行程が割り込まれることを含む表流水の膜浄化方法であ
る。 That is , a first aspect of the present invention is a method for purifying surface water by cross-flow total filtration using a hollow fiber type extraocular or microfiltration membrane module, wherein the hollow fiber type filtration membrane module is removed from the filtration membrane module. line intermittent backwashing at a predetermined pressure range in the permeate or periodic defined pressure control or advance the clean water supplied separately of
At the same time, the permeated water outlet path is
Two locations near the water-side inlet and near the non- permeate water outlet
And the washing water discharge path is provided at two places: a raw water supply path of the filtration membrane module and a cross flow circulation path of non-permeated water.
Branched and installed, the permeation provided at the two locations for each backwash
Of the water outlet path, far from the wash water discharge path
Alternating wash water for backwash from a certain permeate outlet path
Supplying and alternately discharging the washing water from the branched and installed cleaning water discharge path,
Alternatively, regardless of the intermittent backwashing performed while performing the intermittent backwashing, in a state in which the collection of the permeated water is stopped, the filtration membrane module using the raw water with the flushing or backwashing of the filtration membrane module with the raw water is used. A method of purifying surface water including a step of interrupting the flushing process.
【００１５】さらに本発明の第二は、前記第一の方法を
実施するための装置であって、中空糸型限外または精密
濾過膜モジュールを有し、原水を昇圧して前記濾過膜モ
ジュールに供給する原水供給ポンプ、前記原水供給ポン
プのサクション側に非透過水を還流させるクロスフロー
循環経路を有し、前記濾過膜モジュールには原水側入口
の近傍および非透過水出口の近傍に透過水の出口経路を
それぞれ設け、前記透過水の出口経路の合流点の下流に
透過水自動弁および前記透過水を貯留する透過水タンク
を設け、前記透過水タンクの透過水を前記透過水の両出
口経路に分けて戻すための逆洗用ポンプ、逆洗自動弁お
よび逆洗洗浄水供給方向切替手段を有する洗浄水供給経
路を設け、さらに前記濾過膜モジュールの原水供給経路
上であって原水供給ポンプと前記濾過膜モジュールとの
間および前記濾過膜モジュールの非透過水のクロスフロ
ー循環経路上にそれぞれ前記逆洗による洗浄水を排出す
るための洗浄水排出経路を分岐して設けたことを特徴と
する表流水の浄化装置、または前記装置に流量センサー
を有する装置である。Further, a second aspect of the present invention is an apparatus for carrying out the first method, comprising a hollow fiber type ultrafiltration or microfiltration membrane module. A raw water supply pump for supplying, a cross-flow circulation path for recirculating non-permeated water on the suction side of the raw water supply pump, wherein the filtration membrane module has a permeated water near a raw water side inlet and near a non-permeated water outlet; An outlet path is provided, and a permeated water automatic valve and a permeated water tank for storing the permeated water are provided downstream of a junction of the permeated water outlet path. A washing water supply path having a backwashing pump, a backwashing automatic valve and a backwashing washing water supply direction switching means for separating and returning to the raw water supply path on the raw water supply path of the filtration membrane module; A washing water discharge path for discharging the washing water by the back washing is provided between the pump and the filtration membrane module and on the cross flow circulation path of the non-permeated water of the filtration membrane module. Or a device having a flow sensor in the device.
【００１６】なお、前記濾過膜モジュールはその膜材質
が酢酸セルロースであることが好ましく、また中空糸膜
の内側に原水を供給する内圧方式が好ましい。The filtration membrane module is preferably made of cellulose acetate, and is preferably of an internal pressure type for supplying raw water to the inside of the hollow fiber membrane.
【００１７】また、前記逆洗時の前記所定圧力範囲は、
前記濾過膜モジュールの耐圧以下であり、前記通常運転
時の運転圧の実質上１．０倍以上３倍以下とすることが
望ましい。さらに好ましくは、１．３倍以上である。The predetermined pressure range at the time of the back washing is as follows:
It is desirable that the pressure is equal to or less than the pressure resistance of the filtration membrane module and substantially equal to or more than 1.0 times and equal to or less than 3 times the operating pressure during the normal operation. More preferably, it is 1.3 times or more.
【００１８】[0018]
【作用】本発明において、前述の課題は濾過膜表面に付
着した濁質成分の除去を圧力制御若しくは定時間間隔で
行われる前記圧力範囲による逆洗、または前記圧力範囲
で、かつ一定流量の逆洗により行い、その洗浄水を濾過
膜モジュールの原水供給経路に分岐して設置された洗浄
水排出経路より排出させることにより解決される。すな
わち、逆洗により濾過膜表面に付着した濁質成分は内圧
式では中空糸膜の外面側からの逆流により洗浄される
が、洗浄水の排出を前記の洗浄水排出経路より行うこと
により、逆洗時の原水側の水流が通常運転時とは逆の方
向となることから、原水側濾過膜表面に付着した濁質成
分の除去と排出がより良く行われるのである。 また、中
空糸型濾過膜モジュールの透過水出口（逆洗のための透
過水入口）経路を濾過膜モジュールにおいて原水側入口
の近傍および非透過水出口の近傍の二箇所に設け、その
いずれか一方を使用し、片方を封止しておいてもよい
が、通常運転および逆洗の際一方のみを使用する場合
は、前記非透過水出口に近接した位置に設けられたもの
を使用することが好ましい。なお、濾過膜モジュール
は、圧力を一定にしても水温により透過水量が変化す
る。原水に温度変化が生じる場合には、低水温時には一
定圧力で逆洗水を移送してもより高温時より逆洗水量が
低下するため濾過膜モジュールの膜浄化効率も低下す
る。従って、かかる場合には、逆洗ポンプからの流量を
流量センサー等により一定量に調節したり、あるいは逆
洗ポンプに定量ポンプを使用することにより逆洗水量を
一定量にすることが好ましい。In the present invention, the above-mentioned object is to remove turbid components adhering to the surface of the filtration membrane by pressure control or backwashing in the above-mentioned pressure range performed at regular time intervals, or in the above-mentioned pressure range and at a constant flow rate. The problem can be solved by performing washing, and discharging the washing water from a washing water discharge path installed in a branch to a raw water supply path of the filtration membrane module. That is, the turbid component adhered to the filtration membrane surface by the backwashing is washed by the backflow from the outer surface side of the hollow fiber membrane in the internal pressure type. Since the water flow on the raw water side during washing is in the opposite direction to that during normal operation, removal and discharge of turbid components adhering to the surface of the raw water side filtration membrane are performed better . Further, the permeated water outlet (permeated water inlet for backwashing) route of the hollow fiber type filtration membrane module is provided in the filtration membrane module at two places near the raw water side inlet and near the non-permeated water outlet. May be used, and one may be sealed, but when only one is used during normal operation and backwashing, the one provided at a position close to the non-permeated water outlet may be used. preferable. In addition, in the filtration membrane module, the amount of permeated water changes depending on the water temperature even when the pressure is kept constant. When the temperature of the raw water changes, even if the backwash water is transferred at a constant pressure at a low water temperature, the amount of the backwash water is lower than at a higher temperature, so that the membrane purification efficiency of the filtration membrane module also decreases. Therefore, in such a case, it is preferable to adjust the flow rate from the backwash pump to a fixed amount by a flow rate sensor or the like, or to make the backwash water amount constant by using a fixed amount pump for the backwash pump.
【００１９】本発明のさらに好ましい膜浄化方法は、前
記間欠的な逆洗を行う際、各逆洗の度に逆洗による洗浄
水を排出する洗浄水排出経路を下記の濾過膜モジュール
の原水供給経路に分岐して設置された洗浄水排出経路お
よび非透過水のクロスフロー循環経路に分岐して設置さ
れた洗浄水排出経路の２箇所より交互に排出させること
である。これにより、中空糸型濾過膜モジュール内を入
口側、出口側とも十分に逆洗浄することが可能となり、
濁質成分の残留を防ぎ、逆洗による濁質成分の排出が効
率よく行われることとなる。この場合、各逆洗の度に、
前記二箇所に設けられた透過水の出口経路のうち、洗浄
水の排出経路から遠い位置にある透過水の出口経路から
逆洗のための洗浄水を交互に供給することが特に好まし
い。このためには逆洗洗浄水供給方向切替手段を設け
る。なお、本発明における「交互」とは逆洗の度に連続
して２箇所の洗浄水排出経路から洗浄水を排出させるだ
けでなく、１回の逆洗ごとに洗浄水排出経路を切り替え
るものも含まれる。また必要により、二箇所の透過水の
出口経路に同時に洗浄水を供給してもよいことは勿論で
ある。In a further preferred method of purifying a membrane according to the present invention, when the intermittent backwashing is performed, cleaning by backwashing is performed at each backwash.
The cleaning water discharge path, which is provided by branching the cleaning water discharge path that discharges water into the raw water supply path of the following filtration membrane module, and the cleaning water discharge path that is provided by branching into the cross flow circulation path of non-permeated water . It is to discharge from two places alternately. This makes it possible to sufficiently backwash the inside of the hollow fiber type filtration membrane module on both the inlet side and the outlet side,
The suspension of the turbid component is prevented, and the turbid component is discharged efficiently by back washing. In this case, for each backwash,
It is particularly preferable to alternately supply the washing water for backwashing from the outlet passage of the permeated water far from the discharge passage of the washing water among the outlet passages of the permeated water provided at the two places. For this purpose, a backwashing / washing water supply direction switching means is provided. In the present invention, “alternating” means that not only the washing water is continuously discharged from the two washing water discharging paths continuously at every backwashing but also the washing water discharging path is switched every time the backwashing is performed. included. If necessary, the washing water may be simultaneously supplied to two outlet paths of the permeated water.
【００２０】本発明において透過水の流量をＰ、洗浄水
の排出流量をＣとすると、回収率は１００×（Ｐ−Ｃ）
／Ｐ（％）で表され、本発明によれば、回収率９０％以
上９９％以下で運転することが可能である。In the present invention, assuming that the flow rate of the permeated water is P and the discharge flow rate of the washing water is C, the recovery rate is 100 × (PC).
/ P (%), and according to the present invention, it is possible to operate at a recovery rate of 90% or more and 99% or less.
【００２１】本発明の好ましい態様においては、逆洗終
了後通常の原水処理に復帰する前に、原水による濾過膜
モジュールのフラッシングを、前記逆洗よりも短時間行
う。これにより、逆洗では排出に至らなかった残留濁質
成分が強力な原水供給ポンプによる原水フラッシングに
より除去・排出されることとなる。前記フラッシングを
前記逆洗よりも短時間行う理由は、原水の損失を最小限
に抑えるためであり、通常逆洗時間の１／６〜１／１２
程度で十分である。なお、前記フラッシング時に透過水
等を用いた逆洗を併用するとフラッシングの効果が増大
するので、更に好ましい。その際の逆洗水の流れ方向と
しては、通常フラッシングが原水処理時の原水流れ方向
と同一に行われることから、それと同一方向、すなわち
原水側入口の近傍に設けられた透過水出口から逆洗水を
供給し、フラッシングされた原水と共に非透過水のクロ
スフロー循環経路に分岐して設置された洗浄水排出経路
より排出させることが好ましい。なお当然ながら、逆洗
時および原水によるフラッシング時には、透過水の採取
は中断される。また、このような原水による濾過膜モジ
ュールのフラッシングあるいは、逆洗を併用した濾過膜
モジュールのフラッシングは、毎逆洗終了後に行なって
もよく、また逆洗数回後に１回の割合で行ってもよい。
さらに、間欠的逆洗とは独立させて、透過水の採取を停
止した状態で、前記原水による濾過膜モジュールのフラ
ッシングまたは逆洗を伴う原水による濾過膜モジュール
のフラッシング行程として一日に１〜７回、より好まし
くは１から３回、割り込んで実施してもよい。さらにな
お、濾過膜モジュールへの原水の供給を非透過水出口側
に切り替える切替弁システムを設け、原水の処理時およ
び逆洗時におけるフラッシングの際に適宜濾過膜モジュ
ールへの原水供給方向を非透過水出口側に切り替えるこ
ともできる。In a preferred embodiment of the present invention, the flushing of the filtration membrane module with the raw water is performed for a shorter time before the return to the normal raw water treatment after the backwash is completed. As a result, the residual turbid components that have not been discharged by the backwashing are removed and discharged by raw water flushing by a powerful raw water supply pump. The reason why the flushing is performed for a shorter time than the backwashing is to minimize the loss of raw water, and is usually 1/6 to 1/12 of the backwashing time.
A degree is enough. In addition, it is more preferable to use backwashing using permeated water or the like at the time of the flushing, because the effect of flushing increases. As the flow direction of the backwash water at that time, since the flushing is usually performed in the same direction as the flow direction of the raw water at the time of the raw water treatment, the backwash water is backwashed in the same direction, that is, from the permeate outlet provided near the raw water side inlet. It is preferable to supply the water and discharge it from the washing water discharge path which is branched and installed in the cross flow circulation path of the non-permeated water together with the flushed raw water. Naturally, during backwashing and during flushing with raw water, the collection of permeated water is interrupted. The flushing of the filtration membrane module with the raw water or the flushing of the filtration membrane module with backwashing may be performed after each backwash, or may be performed once after several backwashes. Good.
Further, independently of the intermittent backwashing, in a state where the collection of permeated water is stopped, a flushing step of the filtration membrane module with the raw water or a flushing step of the filtration membrane module with the raw water accompanied by the backwash is performed 1 to 7 times a day. The interruption may be performed more preferably one to three times. Furthermore, a switching valve system for switching the supply of the raw water to the filtration membrane module to the non-permeate water outlet side is provided, and the raw water supply direction to the filtration membrane module is appropriately impermeable during the processing of the raw water and the flushing at the time of backwashing. You can also switch to the water outlet side.
【００２２】前記逆洗には、濾過膜モジュールからの透
過水または別途供給される清浄水が用いられる。別途供
給される清浄水として前記濾過膜モジュールからの透過
水をオゾン処理または紫外線照射併用オゾン処理、これ
に続く活性炭処理などの後処理を行ったものであっても
もちろんよい。活性炭処理の後には、活性炭の微粉を除
くため必要に応じてフィルターを設ける。更に逆洗に使
用する透過水または清浄水には、次亜塩素酸塩、二酸化
塩素、塩素、過酸化水素、オゾンなどの酸化性殺菌剤を
注入してもよい。これにより膜面付着物への分解効果も
期待できる。In the back washing, permeated water from a filtration membrane module or separately supplied clean water is used. As the separately supplied clean water, the permeated water from the filtration membrane module may be subjected to post-treatment such as ozone treatment or ozone treatment with ultraviolet irradiation, followed by activated carbon treatment. After the activated carbon treatment, a filter is provided as necessary to remove fine powder of the activated carbon. Further, an oxidizing germicide such as hypochlorite, chlorine dioxide, chlorine, hydrogen peroxide, or ozone may be injected into the permeated water or the clean water used for backwashing. This can also be expected to have the effect of decomposing on the film surface.
【００２３】[0023]
【実施例】以下に、中空糸型濾過膜モジュールであるＵ
Ｆモジュールを用いた場合の本発明の一実施例につい
て、図面を参照して説明するが、精密濾過膜モジュール
を用いても同様に行うことが出来る。図１は本発明に係
わる好ましい表流水の膜浄化方法を実施するための浄化
装置の構成を示す模式図である。 図１において、その構
成は、原水供給側から、逆止弁１０、原水供給ポンプ１
１、並列経路である一方の流量調箇弁１１ａおよび他方
のバイパス弁１１ｂ、ＵＦモジュール１２、原水側入口
１２ａ、非透過水出口１２ｂ、中空糸束１２ｃ、ＵＦモ
ジュール１２内の透過水流路１２ｄ、ＵＦモジュール１
２に原水側入り口１２ａの近傍および非透過水出口１２
ｂの近傍の二箇所に設けた透過水出口１２ｅ、１２ｆを
有する透過水出口経路、逆洗洗浄水供給方向切替手段と
しての三方切替弁１２ｇ、透過水自動弁１３、透過水を
蓄積するための透過水タンク１７、蓄積された透過水を
ＵＦモジュール１２の透過水出口側に戻して逆洗を行う
ためのポンプ１８、逆洗自動弁１９からなっている。ま
た、洗浄水排出自動弁１４ａ、１４ｂを有する洗浄水排
出経路１５ａ、１５ｂを原水供給ポンプ１１とＵＦモジ
ュール１２の原水側入口１２ａとの間の原水供給経路お
よび非透過水の循環するクロスフロー循環経路１６の２
箇所にそれぞれ分岐して接続している。また、クロスフ
ロー循環経路１６には弁１６ａを設けている。なお、逆
洗ポンプ１８の流量を調節する流量センサー１を逆洗自
動弁１９と三方切替弁１２ｇとの間に有してもよい。DESCRIPTION OF THE PREFERRED EMBODIMENTS A hollow fiber type filtration membrane module U
One embodiment of the present invention in which an F module is used will be described with reference to the drawings. However, the same operation can be performed using a microfiltration membrane module. Figure 1 is engaged with the present invention
Purification for implementing the preferred surface water film removal method Waru
Schematic diagram illustrating the configuration of a device. In FIG.
From the raw water supply side, check valve 10, raw water supply pump 1
1. One flow control valve 11a which is a parallel path and the other
Bypass valve 11b, UF module 12, the raw water side inlet 12a, a non-permeate outlet 12b, the hollow fiber bundle 12c, permeate flow path 12d of the UF module 12, UF Module 1
2 shows the vicinity of the raw water side inlet 12a and the non-permeated water outlet 12
b permeate outlet 12e provided in two locations in the vicinity of the 12f
A permeate outlet path , a three-way switching valve 12g as a backwashing water supply direction switching means, a permeate automatic valve 13, a permeate tank 17 for accumulating permeate, and permeation of the accumulated permeate through the UF module 12. It comprises a pump 18 for returning back to the water outlet side for backwashing, and a backwash automatic valve 19 . Ma
In addition, the cleaning water discharge paths 15a and 15b having the automatic cleaning water discharge valves 14a and 14b are connected to the raw water supply path between the raw water supply pump 11 and the raw water side inlet 12a of the UF module 12, and the non-permeated water. 2 of cross flow circulation path 16 for circulating
It is branched and connected to each location . The cross flow circulation path 16 is provided with a valve 16a. The flow sensor 1 for adjusting the flow rate of the backwash pump 18 may be provided between the automatic backwash valve 19 and the three-way switching valve 12g.
【００２４】この処理システムの運転は次のようにして
行われる。通常運転に際しては、透過水自動弁１３を
開、洗浄水排出自動弁１４ａ、１４ｂ、逆洗自動弁１９
は共に閉とし、ポンプ１８を停止状態におく。このよう
にして、逆止弁１０を経て導入された河川水等の原水
は、原水供給ポンプ１１により昇圧されて、流量調節弁
１１ａを経由しＵＦモジュール１２に供給される。ＵＦ
モジュール１２では、限外濾過膜の濾過作用により濁質
成分を除去した透過水を、透過水出口１２ｅ、１２ｆ、
三方切替弁１２ｇ、透過水自動弁１３を通して透過水タ
ンク１７に蓄積する。なお、透過水出口１２ｅ、１２ｆ
は両者を同時に使用してもよく、片方のみ使用してもよ
く、さらには逆洗の度に交互に使用してもよい。この通
常運転の間、非透過水はクロスフロー循環経路１６を通
して、原水の流入量に対して好ましくはゼロを越え６倍
以下程度の量のクロスフローが行われるが、透過水量は
原水量に等しい。The operation of the processing system is performed as follows. During normal operation, the automatic permeated water valve 13 is opened, the automatic flush water discharge valves 14a, 14b,
Are closed, and the pump 18 is stopped. In this way, raw water such as river water introduced through the check valve 10 is pressurized by the raw water supply pump 11 and supplied to the UF module 12 via the flow control valve 11a. UF
In the module 12, the permeated water from which the turbid components have been removed by the filtration action of the ultrafiltration membrane is supplied to the permeated water outlets 12e, 12f,
It accumulates in the permeated water tank 17 through the three-way switching valve 12g and the permeated water automatic valve 13. The permeated water outlets 12e, 12f
May be used at the same time, only one of them may be used, or they may be used alternately at each backwash. During this normal operation, the non-permeated water cross-flows through the cross-flow circulation path 16 preferably in an amount of more than zero and about six times or less with respect to the inflow of raw water, but the amount of permeated water is equal to the amount of raw water. .
【００２５】逆洗は、例えば３０分ないし１時間程度の
定時間間隔で３０〜６０秒の間行われ、次の２種類の逆
洗を行う。逆洗モード（１）は、原水供給ポンプ１１を
停止すると共に透過水自動弁１３を閉、洗浄水排出自動
弁１４ｂ、逆洗自動弁１９は共に開とし、ポンプ１８を
運転する。また三方切替弁１２ｇは透過水出口１２ｆの
方に開としておく。このようにして、透過水タンク１７
に蓄積された透過水の一部を利用してＵＦモジュール１
２に対する逆洗が透過水出口１２ｆからの洗浄水により
行われ、逆洗により中空糸膜の内表面からはぎとられた
濁質成分は、洗浄水排出自動弁１４ｂを通してシステム
外に排出される。このとき弁１６ａは閉とすることが好
ましい。洗浄水量は洗浄水排出水量に等しい。逆洗モー
ド（１）により１２ａ付近の濁質が除去できる。尚、こ
の場合において逆洗流量センサー１を設置することによ
り逆洗流量を一定量に維持することができ、またはポン
プ１８を定量ポンプとしても、一定量の逆洗水を供給す
ることができる。The backwashing is performed at regular time intervals of, for example, about 30 minutes to 1 hour for 30 to 60 seconds, and the following two types of backwashing are performed. In the backwash mode (1), the raw water supply pump 11 is stopped, the permeated water automatic valve 13 is closed, the wash water discharge automatic valve 14b, and the backwash automatic valve 19 are both opened, and the pump 18 is operated. The three-way switching valve 12g is opened toward the permeated water outlet 12f. Thus, the permeated water tank 17
Module 1 using part of the permeated water accumulated in
Backwashing of 2 is carried out with washing water from the permeated water outlet 12f, and the turbid component stripped from the inner surface of the hollow fiber membrane by backwashing is discharged out of the system through the washing water discharge automatic valve 14b. At this time, the valve 16a is preferably closed. The flush water volume is equal to the flush water discharge volume. The turbidity around 12a can be removed by the backwash mode (1). In this case, by installing the backwash flow sensor 1, the backwash flow can be maintained at a constant amount, or a constant amount of backwash water can be supplied even when the pump 18 is used as a fixed amount pump.
【００２６】しかし、１２ｂ付近の濁質はいまだ十分に
除去できていないため、引き続き、逆洗モード（２）に
入る。三方切替弁１２ｇは透過水出口１２ｅの方に開及
び、循環経路自動弁１６ａ、透過水自動弁１３を閉とし
ておく。そして洗浄水は透過水出口１２ｅを経由してＵ
Ｆモジュール１２に入り、濁質成分を含む洗浄水は同様
に洗浄水排出経路１５ａ、同弁１４ａを経由してシステ
ム外に排出される。即ち、逆洗の度に、逆洗モード
（１）と逆洗モード（２）により運転することにより、
二箇所に設けた透過水出口（経路）１２ｆ，１２ｅのう
ち、洗浄水の排出経路１５ｂ，１５ａから遠い位置にあ
る透過水出口（経路）１２ｆ，１２ｅから逆洗のための
洗浄水を交互に供給し、排出経路１５ｂ，１５ａより交
互に排出されることになる。逆洗モード（２）終了後、
前記原水の処理の状態に復帰するが、その前に透過水自
動弁１３、循環経路自動弁１６ａは閉、洗浄水排出弁１
４ａは開で、逆洗自動弁１９を開、ポンプ１８を運転さ
せ、三方切替弁１２ｇおよび透過水出口１２ｅを経由し
て透過水による逆洗を行いながら、ポンプ１１により原
水をフラッシングさせ洗浄水排出弁１４ａより排出させ
ると、前記逆洗のみでは排出されなかったモジュールの
原水側濁質成分が排出され易くなるので、極めて効果的
である。この場合、逆洗をしないで、単に原水によるフ
ラッシングを行ってもよいが、前記のように逆洗と共に
原水をフラッシングさせることがより好ましい。これら
のフラッシングは原水の損失が大きくならない程度の時
間、すなわち前記フラッシングを伴わない逆洗時間の１
／６〜１／１２で十分である。なおフラッシングを行う
際には、バイパス弁１１ｂを開とし、原水を一時的に大
量に流すことが好ましい。バイパス弁１１ｂはフラッシ
ング時以外は閉とする。通常の原水処理時に使用する流
量調節弁１１ａとフラッシング時に使用するバイパス弁
１１ｂの両者の代わりに、原水供給ポンプ１１としてイ
ンバーター制御機能をもたせたものを使用することによ
り、それぞれの流量調節をポンプの回転数の変化により
行ってもよい。However, since the turbidity near 12b has not been sufficiently removed yet, the operation enters the backwash mode (2). The three-way switching valve 12g is opened toward the permeated water outlet 12e, and the circulation path automatic valve 16a and the permeated water automatic valve 13 are closed. Then, the washing water is supplied to the U
After entering the F module 12, the washing water containing the turbid component is similarly discharged to the system via the washing water discharge path 15a and the valve 14a.
Is discharged outside the system . In other words, every time a backwash is performed,
By operating in (1) and backwash mode (2),
Permeate outlets (paths) 12f and 12e provided at two locations
At a position far from the washing water discharge paths 15b and 15a.
Permeate outlets (paths) 12f and 12e for backwash
The washing water is supplied alternately and exchanged from the discharge paths 15b and 15a.
They will be discharged together. After the backwash mode (2) ends,
Before returning to the raw water treatment state, the permeated water automatic valve 13 and the circulation path automatic valve 16a are closed and the washing water discharge valve 1
4a is open, the backwashing automatic valve 19 is opened, the pump 18 is operated, and the backwater is flushed by the pump 11 while backwashing with the permeated water via the three-way switching valve 12g and the permeated water outlet 12e. When discharged through the discharge valve 14a, the raw water-side turbid component of the module that has not been discharged only by the backwashing is easily discharged, which is extremely effective. In this case, flushing with raw water may be performed without backwashing, but it is more preferable to flush the raw water together with backwashing as described above. These flushing times are such that the loss of raw water does not increase, that is, one of the backwashing times without the flushing.
/ 6 to 1/12 is sufficient. When performing flushing, it is preferable to open the bypass valve 11b and temporarily flow a large amount of raw water. The bypass valve 11b is closed except during flushing. By using a raw water supply pump 11 having an inverter control function instead of both the flow control valve 11a used during normal raw water treatment and the bypass valve 11b used during flushing, the flow control of each pump is performed. This may be performed by changing the rotation speed.
【００２７】図１の膜浄化装置の変形として、図２の装
置を使用することもできる。図２では１１ｃ〜１１ｆか
らなる切替弁システムを設け、前記原水によるフラッシ
ングまたは透過水による逆洗を伴うフラッシングを行う
に当たり原水の通液方向をＵＦモジュール１２の原水側
入口１２ａのみならず、非透過水出口１２ｂ側からも行
えるようにしたものである。図２の装置においては、通
常の原水処理時には弁１１ｅ、１１ｄを開とし、１１
ｃ、１１ｆを閉とする。原水によるフラッシングを１２
ａ側から行うには、１１ｅを開、１１ｃ、１１ｆを閉と
し、１２ｂ側から行うには１１ｃを開とし、１１ｄ、１
１ｅを閉とすれば足りる。なお、切替弁システムを用い
ることにより原水を処理する際にも、適宜原水の濾過膜
モジュールへの供給方向を１２ｂ側にすることもでき
る。また逆洗洗浄水供給方向切替手段として図１の二方
向切替弁１２ｇの代わりに弁１２ｈ、１２ｉを用いるこ
ととし、更に殺菌剤注入ポンプ１８ａを取り付けた。そ
の他は図１と同様である。As a modification of the membrane purifying apparatus of FIG. 1, the apparatus of FIG. 2 can be used. In FIG. 2, a switching valve system including 11 c to 11 f is provided, and in performing the flushing with the raw water or the flushing with the backwash with the permeated water, the flow direction of the raw water is not only the raw water side inlet 12 a of the UF module 12 but also the non-permeate. This can be performed also from the water outlet 12b side. In the apparatus shown in FIG. 2, during normal raw water treatment, the valves 11e and 11d are opened, and
Close c and 11f. 12 flushing with raw water
To perform from the a side, open 11e, close 11c and 11f, and to perform from the 12b side, open 11c, 11d, 1d
It is enough to close 1e. Incidentally, when processing raw water by <br/> Rukoto using the switching valve system, or may be the direction of supplying the appropriate raw water to the filtration membrane module 12b side. Further, valves 12h and 12i were used as the backwashing / washing water supply direction switching means instead of the two-way switching valve 12g in FIG. 1, and a germicide injection pump 18a was further attached. Others are the same as FIG.
【００２８】以下、図１の浄化装置を用いて行った各種
の測定結果を参照しながら説明する。図５、６は、横軸
がそれぞれ運転時間、運転日数、縦軸がフラックスとも
称される単位面積・時間当たりの流量（以下、単に「流
量」と略す、（図には流束と示す）、単位はリットル／
ｍ２・ｈ）但し１５℃、１ｋｇ／ｃｍ２換算）変化との
関係を示した図である。運転条件としては、ＵＦモジュ
ール１２の材質に分画分子量１５０，０００の酢酸セル
ロースを使用し、中空糸内径０．８ｍｍ、膜面積５
ｍ２、平均運転圧０．５ｋｇ／ｃｍ２、循環流水量５０
０リットル／ｈ、逆洗圧１．０Ｋｇ／ｃｍ２、回収率９
５％とした。図５は片側逆洗のみを行った場合の参考
図、図６は交互逆洗（実施例）（黒丸印）を行った場合
と片側逆洗（参考例）（白丸印）を行った場合との比較
を示す図である。 Hereinafter, a description will be given with reference to the results of various measurements performed using the purification apparatus of FIG. 5 and 6, the horizontal axis represents the operating time and the number of operating days, and the vertical axis represents the flow rate per unit area / time (hereinafter simply referred to as “flow rate”, also referred to as flux). , Unit is liter /
m 2 · h), where 15 ° C., 1 kg / cm 2 conversion). The operating conditions were as follows. Cellulose acetate having a molecular weight cut off of 150,000 was used as the material of the UF module 12, the inner diameter of the hollow fiber was 0.8 mm, and the membrane area was 5
m 2 , average operating pressure 0.5 kg / cm 2 , circulating water flow 50
0 liter / h, backwash pressure 1.0 kg / cm 2 , recovery rate 9
5%. Fig. 5 is a reference when only one-sided backwash is performed.
Figures and 6 show alternate backwashing (Example) (black circles)
Comparison with the case of one-side backwash (reference example) (open circles)
FIG.
【００２９】図６には、逆洗後における通常運転時の透
過水の流量の変化の状態を示す。実施例（黒丸印）は、
逆洗毎に透過水出口１２ｅおよび１２ｆから交互に洗浄
水を供給し、供給した口より遠い位置にある排出経路か
ら排出するようにして、洗浄水排出経路１５ａと１５ｂ
とを交互に使用して逆洗を行った場合（交互逆洗）と、
参考例（白丸印）として、前記図５に示す参考例（黒丸
印）と同様に、洗浄水排出経路１５ｂのみを用いて逆洗
を行った場合（片側逆洗）との通常運転時の透過水の流
量の変化を示した。図６から分かるように、両排出経路
を交互に使用した方が、流量低下の小さいことが分か
る。FIG. 6 shows the transparency during normal operation after backwashing .
The state of a change in the flow rate of supercharging is shown. Examples (black circles)
The washing water is alternately supplied from the permeated water outlets 12e and 12f for each backwash, and is discharged from a discharge path located at a position farther from the supplied water, so that the washing water discharge paths 15a and 15b are provided.
When backwashing is performed using alternately (and alternate backwashing),
As a reference example (open circle), as in the reference example (black circle) shown in FIG. 5 described above, the transmission during normal operation when backwashing was performed using only the washing water discharge path 15b (one-side backwash). The change of water flow was shown. As can be seen from FIG. 6, it can be seen that the flow rate decrease is smaller when both the discharge paths are used alternately.
【００３０】図５は、前述のように参考図であり、図中
の黒丸印は、図６に示す参考例と同じ条件（片側逆洗）
での結果を示す、白丸印は、前述の図４の膜浄化装置を
用いて同じ条件で運転した比較例の結果を示し、矢印は
逆洗した時点を示す。図５から明らかなように、参考例
（黒九印）の流量の低下は殆ど見られないのに対して、
比較例（白丸印）の場合は、逆洗を行っても濁質成分の
除去が不十分で目詰りを生じ、時間経過と共に流量が次
第に低下している。すなわち、図５および図６から、実
施例（交互逆洗）の場合は、従来の図４に示す膜浄化装
置を用いた比較例（片側逆洗）の場合に比較し、流量の
低下は長時間に渡り少なく、本願発明の装置を用い膜洗
浄方法によれば、長時間の運転をすることができるとい
う優れた効果を有している。 FIG . 5 is a reference diagram as described above .
Indicates the same conditions as in the reference example shown in FIG. 6 (one-sided backwashing).
, The white circles indicate the results of the comparative example operated under the same conditions using the membrane purifying apparatus of FIG. 4 described above, and the arrows indicate the time of back washing. As is clear from FIG. 5, the reference example
(Kuro Nine), while there is almost no decrease in flow rate,
In the case of the comparative example (open circles) , even when the back washing was performed, the removal of the turbid components was insufficient and clogging occurred, and the flow rate gradually decreased with time. That is, from FIG. 5 and FIG.
In the case of the embodiment (alternate backwashing), the conventional membrane purifying device shown in FIG.
Flow rate compared to the comparative example (one-sided backwash)
The decrease is small over a long period of time.
According to the purification method, it can be operated for a long time
It has an excellent effect.
【００３１】[0031]
【発明の効果】以上ＵＦモジュールを例にして説明して
きたように、本発明による膜浄化方法およびその装置を
用いることにより、実質的に全量濾過に近い方式で無駄
に排出される洗浄水量が非常に少なく、高回収率で表流
水の膜浄化が達成できる。また逆洗が効率的に行われる
結果、流量の低下が小さいので長期間の運転も可能であ
る。また使用するＵＦモジュールまたは精密濾過膜モジ
ュールに対するクロスフロー量（循環量）も従来方式に
比べてはるかに少なくて済むので、ＵＦモジュールまた
は精密濾過モジュールに原水を供給すると共に、クロス
フローを行うためのポンプも大容量のものを必要とせず
小型のものでよく、ポンプの電力消費量を大幅に減らす
ことが出来る。従って、従来の大循環量によるクロスフ
ローに比しランニングコストが小さくなる。As described above with reference to the UF module as an example, by using the membrane purification method and the apparatus according to the present invention, it is possible to reduce the amount of waste water discharged in a manner substantially similar to the total filtration. And the purification of surface water can be achieved with a high recovery rate. In addition, as a result of efficient backwashing, a decrease in the flow rate is small, so that long-term operation is possible. Also, since the cross-flow amount (circulation amount) for the UF module or the microfiltration membrane module to be used is much smaller than that of the conventional method, the raw water is supplied to the UF module or the microfiltration module and the cross-flow is performed. The pump does not need to have a large capacity and can be small, and the power consumption of the pump can be greatly reduced. Therefore, the running cost is reduced as compared with the conventional cross flow with a large circulation amount.
【図１】 本発明による腰浄化方法を実施するための浄
化装置の構成を示す模式図である。FIG. 1 is a schematic view showing a configuration of a purifying device for performing a waist purifying method according to the present invention.
【図２】 本発明による膜浄化方法を実施するための浄
化装置の別の構成を示す模式図である。FIG. 2 is a schematic diagram showing another configuration of a purification device for performing the membrane purification method according to the present invention.
【図３】 ＵＦモジュール利用による従来の浄化方法を
実施するための構成を示す模式図である。FIG. 3 is a schematic diagram showing a configuration for implementing a conventional purification method using a UF module.
【図４】 ＵＦモジュール利用による従来の浄化方法を
実施するための構成を示す模式図である。FIG. 4 is a schematic diagram showing a configuration for implementing a conventional purification method using a UF module.
【図５】 図６に示すものと同じ条件で、かつ片側逆洗
で運転した場合の運転時間と流量の関係を示した図であ
る。FIG. 5: Under the same conditions as those shown in FIG .
In is a diagram showing the operating time and the flow rate relationship when driving.
【図６】 図１に示された構成において、各種条件を設
定して運転した場合の交互逆洗と片側逆洗の流量の低下
に及ぼす影響を比較した図である。FIG. 6 sets various conditions in the configuration shown in FIG . 1;
It is the figure which compared the influence which it has on the fall of the flow volume of alternate backwashing and one-sided backwashing in the case of fixed operation .
１ 逆洗流量センサー １０ 逆止弁 １１，１８，１８ａ ポンプ １１ｃ，１１ｄ，１１ｅ，１１ｆ 弁 １２ ＵＦモジュール １２ａ 原水入口 １２ｂ 原水出口 １２ｃ 透過水側 １２ｄ 中空糸束 １２ｅ，ｆ 透過水出口 １２ｇ 三方切替弁 １３ 透過水自動弁 １４ａ，ｂ 洗浄水排出自動弁 １５ａ，ｂ 洗浄水排出経路 １６ 循環経路 １７ 透過水タンク １９ 逆洗自動弁 Reference Signs List 1 backwash flow sensor 10 check valve 11, 18, 18a pump 11c, 11d, 11e, 11f valve 12 UF module 12a raw water inlet 12b raw water outlet 12c permeated water side 12d hollow fiber bundle 12e, f permeated water outlet 12g three-way switching valve 13 Automatic permeated water valve 14a, b Automatic cleaning water discharge valve 15a, b Cleaning water discharge path 16 Circulation path 17 Permeated water tank 19 Backwash automatic valve
───────────────────────────────────────────────────── フロントページの続き (56)参考文献 特開 平４−310220（ＪＰ，Ａ) 特開 平２−8465（ＪＰ，Ａ) 特開 平１−104309（ＪＰ，Ａ) 特開 昭54−71085（ＪＰ，Ａ) 特開 昭56−24006（ＪＰ，Ａ) 特開 昭52−26379（ＪＰ，Ａ) 特開 昭53−17581（ＪＰ，Ａ) 実開 昭62−187606（ＪＰ，Ｕ) ──────────────────────────────────────────────────続 き Continuation of the front page (56) References JP-A-4-310220 (JP, A) JP-A-2-8465 (JP, A) JP-A-1-104309 (JP, A) JP-A-54- 71085 (JP, A) JP-A-56-24006 (JP, A) JP-A-52-26379 (JP, A) JP-A-53-17581 (JP, A) Japanese Utility Model Laid-Open No. 62-187606 (JP, U)
Claims (11)
ルを用いてクロスフロー全量濾過により表流水を浄化す
る方法において、前記中空糸型濾過膜モジュールを該濾
過膜モジュールからの透過水または別途供給される清浄
水により圧力制御またはあらかじめ定められた周期で所
定圧力範囲で間欠的な逆洗を行うに際し、前記濾過膜モ
ジュールに透過水出口経路を原水側入口の近傍および非
透過水出口の近傍の二箇所に設け、洗浄水排出経路を前
記濾過膜モジュールの原水供給経路および非透過水のク
ロスフロー循環経路の二箇所に分岐して設置し、各逆洗
の度に前記二箇所に設けた透過水の出口経路のうち、洗
浄水の排出経路から遠い位置にある透過水の出口経路か
ら逆洗のための洗浄水を交互に供給し、前記分岐して設
置された洗浄水排出経路より交互に排出させることを特
徴とする表流水の膜浄化方法。1. A method for purifying surface water by cross-flow total filtration using a hollow fiber type ultrafiltration or microfiltration membrane module, wherein the hollow fiber type filtration membrane module is supplied with permeated water from the filtration membrane module or separately supplied. When performing pressure control or intermittent backwashing in a predetermined pressure range at a predetermined cycle with the clean water to be removed, the filtration membrane module is used.
The permeated water outlet route to the joule
It is provided at two locations near the permeate outlet, and the washing water discharge route is branched and installed at the two locations of the raw water supply route of the filtration membrane module and the cross-flow circulation route of the non-permeate water. Washing
Out of the permeated water outlet routes provided at the two locations
Is the permeated water outlet path far from the purified water discharge path?
Washing water for backwashing is alternately supplied from the washing water outlet, and is alternately discharged from the washing water discharge path provided in a branched manner.
おいて、間欠的な逆洗時の逆洗水量を水温に依らず一定
量にすることを特徴とする表流水の膜浄化方法。2. A surface water film cleaning method according to claim 1, surface water of a membrane purification method, characterized in that a certain amount regardless of the backwash water during intermittent backwashing water temperature.
化方法において、逆洗による洗浄水を洗浄水排水経路よ
り排出させた後、透過水の採取を停止した状態で前記逆
洗よりも短時間原水による濾過膜モジュールのフラッシ
ングを行うことを含む表流水の膜浄化方法。3. The method of purifying surface water according to claim 1 , wherein the backwash water is discharged from the backwater drainage channel, and then the backwash is performed in a state where the collection of permeated water is stopped. A method for purifying membrane of surface water, comprising flushing a filtration membrane module with raw water for a short time.
方法において、逆洗による洗浄水を洗浄水排水経路より
排出させた後、透過水の採取を停止した状態で前記逆洗
よりも短時間更に逆洗を継続しながら原水による濾過膜
モジュールのフラッシングを行うことを含む表流水の膜
浄化方法。4. The method for purifying surface water according to claim 1 or 2 , wherein after the washing water by backwashing is discharged from the washing water drainage path, the collection of permeated water is stopped and then the backwashing is performed. A membrane purification method for surface water comprising flushing a filtration membrane module with raw water while continuing backwashing for a short time.
化方法において、間欠的に行われる逆洗とは無関係に、
透過水の採取を停止した状態で、原水による濾過膜モジ
ュールのフラッシングまたは逆洗を伴う原水による濾過
膜モジュールのフラッシング行程が割り込まれることを
含む表流水の膜浄化方法。5. The method of purifying surface water according to claim 1 , wherein the backwashing is performed intermittently.
While the collection of permeated water is stopped, the process of flushing the filtration membrane module with raw water or interrupting the flushing process of the filtration membrane module with raw water that involves backwashing is performed.
A method for purifying membranes containing surface water.
流水の膜浄化方法において、前記濾過膜モジュールは、
その膜材質が酢酸セルロースであることを特徴とする表
流水の膜浄化方法。6. The surface water film cleaning method according to any one of claims 1 to 5, wherein the filtration membrane module,
A membrane purification method for surface water, wherein the membrane material is cellulose acetate.
流水の膜浄化方法において、前記中空糸型濾過膜モジュ
ールを用いたクロスフロー濾過は、内圧方式であること
を特徴とする表流水の膜浄化方法。7. The method for purifying surface water according to any one of claims 1 to 5 , wherein the cross-flow filtration using the hollow fiber type filtration membrane module is an internal pressure method. Surface water purification method.
法を実施するための装置であって、中空糸型限外または
精密濾過膜モジュールを有し、原水を昇圧して前記濾過
膜モジュールに供給する原水供給ポンプ、前記原水供給
ポンプのサクション側に非透過水を還流させるクロスフ
ロー循環経路を有し、前記濾過膜モジュールには原水側
入口の近傍および非透過水出口１の近傍に透過水の出口
経路をそれぞれ設け、前記透過水の出口経路の合流点の
下流に透過水自動弁および前記透過水を貯留する透過水
タンクを設け、前記透過水タンクの透過水を前記透過水
の両出口経路に分けて戻すための逆洗用ポンプ、逆洗自
動弁および逆洗洗浄水供給方向切替手段を有する洗浄水
供給経路を設け、さらに前記濾過膜モジュールの原水供
給経路上であって原水供給ポンプと前記濾過モジュール
との間および前記濾過膜モジュールの非透過水のクロス
フロー循環経路上にそれぞれ前記逆洗による洗浄水を排
出するための洗浄水排出経路を分岐して設けたことを特
徴とする表流水の浄化装置。8. An apparatus for performing the method according to any one of claims 1 to 5 , comprising a hollow fiber type ultra- or microfiltration membrane module, and pressurizing raw water to perform the filtration. A raw water supply pump for supplying to the membrane module, a cross flow circulation path for circulating non-permeated water on a suction side of the raw water supply pump, and a vicinity of the raw water side inlet and a non-permeated water outlet 1 in the filtration membrane module; A permeate outlet path is provided, and a permeate automatic valve and a permeate tank for storing the permeate are provided downstream of a junction of the permeate outlet path. A washing water supply path having a backwashing pump, a backwash automatic valve and a backwashing washing water supply direction switching means for returning separately to both outlet paths, and further on the raw water supply path of the filtration membrane module. original A washing water discharge path for discharging the washing water by the back washing is provided between the water supply pump and the filtration module and on the cross flow circulation path of the non-permeated water of the filtration membrane module. Characteristic surface water purification equipment.
する請求項８記載の表流水の浄化装置。9. The surface water purifying apparatus according to claim 8 , further comprising a backwash flow sensor.
出経路の分岐と原水供給ポンプとの間の原水供給経路上
に、並列経路を設け、前記並列経路の一方にバイパス弁
を、もう一方に流量調節弁をそれぞれ設置した請求項８
または９記載の表流水の浄化装置。10. A parallel path is provided on a raw water supply path between a branch of a wash water discharge path provided on the raw water supply path and a raw water supply pump, a bypass valve is provided on one of the parallel paths, and the other is provided on the other side. 8. a flow control valve installed respectively
Or a surface water purification apparatus according to 9 .
と洗浄水排出経路の分岐との間に濾過膜モジュールへの
原水の供給方向を濾過膜モジュールの非透過水出口側に
切り替えるための切替弁システムを設けた請求項８〜１
０のいずれか１項に記載の表流水の浄化装置。11. A switch for switching the supply direction of raw water to the filtration membrane module to the non-permeate water outlet side of the filtration membrane module on the raw water supply path and between the parallel path and the branch of the washing water discharge path. 8. A valve system according to claim 8, further comprising a valve system.
0. The apparatus for purifying surface water according to any one of 0 .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6027444A JP2724673B2 (en) | 1993-01-29 | 1994-01-31 | Surface water purification method and device therefor |
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5-34260 | 1993-01-29 | ||
| JP3426093 | 1993-01-29 | ||
| JP6027444A JP2724673B2 (en) | 1993-01-29 | 1994-01-31 | Surface water purification method and device therefor |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH06277664A JPH06277664A (en) | 1994-10-04 |
| JP2724673B2 true JP2724673B2 (en) | 1998-03-09 |
Family
ID=26365359
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6027444A Expired - Lifetime JP2724673B2 (en) | 1993-01-29 | 1994-01-31 | Surface water purification method and device therefor |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP2724673B2 (en) |
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Families Citing this family (37)
| Publication number | Priority date | Publication date | Assignee | Title |
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Family Cites Families (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5226379A (en) * | 1975-08-25 | 1977-02-26 | Asahi Chem Ind Co Ltd | Method of washing ultrafiltration membranes |
| JPS5317581A (en) * | 1976-07-31 | 1978-02-17 | Toshiba Machine Co Ltd | Method and apparatus for cleaning semipermeable membrane |
| JPS5471085A (en) * | 1977-11-16 | 1979-06-07 | Yuasa Battery Co Ltd | Filtration apparatus |
| JPS5624006A (en) * | 1979-08-06 | 1981-03-07 | Ebara Infilco Co Ltd | Maintainance method of capacity of permeable membrane in membrane separation |
| JPS62187606U (en) * | 1986-05-21 | 1987-11-28 | ||
| JPH01104309A (en) * | 1987-10-16 | 1989-04-21 | Akua Runesansu Kijiyutsu Kenkyu Kumiai | Washing method for membrane module |
| JPH028465A (en) * | 1988-06-28 | 1990-01-11 | Mitsubishi Rayon Co Ltd | Method and apparatus for cleaning swimming pool water |
| JPH04310220A (en) * | 1991-04-05 | 1992-11-02 | Takaoka Electric Mfg Co Ltd | Method for cleaning hollow fiber membrane |
-
1994
- 1994-01-31 JP JP6027444A patent/JP2724673B2/en not_active Expired - Lifetime
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
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