JPH081158A - Method for operating water purification system and water purifier - Google Patents
Method for operating water purification system and water purifierInfo
- Publication number
- JPH081158A JPH081158A JP15789394A JP15789394A JPH081158A JP H081158 A JPH081158 A JP H081158A JP 15789394 A JP15789394 A JP 15789394A JP 15789394 A JP15789394 A JP 15789394A JP H081158 A JPH081158 A JP H081158A
- Authority
- JP
- Japan
- Prior art keywords
- water
- hollow fiber
- purification system
- fiber membrane
- water purification
- 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.)
- Granted
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、中空糸膜モジュールを
用いた水浄化システムの運転方法に関し、更に詳しく
は、原水濁度の変動に対応した回収率の制御により、透
過水量を一定値にして透過水を得、同時に中空糸膜の膜
状態を一定に維持することにより中空糸膜の寿命延長を
図ることができる水浄化システムの運転方法ならびに水
浄化装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for operating a water purification system using a hollow fiber membrane module. More specifically, the permeated water amount is controlled to a constant value by controlling the recovery rate corresponding to fluctuations in raw water turbidity. The present invention relates to a method for operating a water purification system and a water purification device that can extend the life of a hollow fiber membrane by obtaining permeated water and simultaneously maintaining the membrane state of the hollow fiber membrane constant.
【０００２】[0002]
【従来の技術】最近、膜分離技術を適用する水浄化シス
テムとして、中空糸膜モジュールを用いたクロスフロー
濾過が行われている。ここにクロスフロー濾過とは、中
空糸膜の膜面（原水供給側分離膜面）の一方に原水を供
給し、中空糸膜を透過した透過水を分離膜の他方の膜面
（透過水側分離膜面）から回収する際、原水供給側分離
膜面に平行に原水を流して濾過を行うことにより、中空
糸膜表面に付着した原水に含まれていた濁質物質をその
膜表面からはぎ取る効果を有する濾過方法をいう。しか
し、原水中に含まれる濁質物質によって中空糸膜に目詰
まりが発生し、濾過時間の経過による濁質物質の分離膜
表面への積層は、クロスフロー濾過によっても解消され
ず、水浄化システムの運転中断の直接的な原因となるた
め、目詰まりを解消し、あるいは予防するために、一般
的に逆流洗浄（以下、逆洗と称す。）が行われている。2. Description of the Related Art Recently, cross-flow filtration using a hollow fiber membrane module has been performed as a water purification system to which a membrane separation technique is applied. Cross-flow filtration here means that raw water is supplied to one of the hollow fiber membrane surfaces (raw water supply side separation membrane surface), and the permeated water that has permeated through the hollow fiber membrane is passed through the other membrane surface (permeate side). When collecting from the separation membrane surface), the raw water is fed in parallel to the separation membrane surface of the raw water supply side to perform filtration, so that the suspended substances contained in the raw water adhering to the hollow fiber membrane surface are stripped from the membrane surface. A filtration method that has an effect. However, the hollow fiber membranes are clogged by the suspended substances contained in the raw water, and the accumulation of suspended substances on the surface of the separation membrane due to the passage of filtration time cannot be eliminated by cross-flow filtration. In order to eliminate or prevent the clogging, it is generally a direct cause of the operation interruption of backwashing, and therefore backwashing (hereinafter referred to as backwashing) is generally performed.
【０００３】このような、逆洗を含むクロスフロー濾過
による水浄化システムの運転方法として、例えば、特開
平４−２４７２２６号公報には、原水の水質検知部を設
け、変化する原水の水質を確認し、透過水量が所定時間
内に低下傾向の時に膜の逆洗条件を変更して、予め設定
した透過水量となるように自動調整する方法が開示され
ている。さらに、特開平５−３１７６６０号公報には、
複数の膜分離装置を使用し、検出した原水濁度に基づき
逆洗間隔を調節する装置が開示されている。As a method of operating such a water purification system by cross-flow filtration including backwashing, for example, in Japanese Patent Laid-Open No. 4-247226, a raw water quality detection unit is provided to check the changing raw water quality. However, there is disclosed a method in which the backwashing condition of the membrane is changed when the amount of permeated water tends to decrease within a predetermined time, and the amount of permeated water is automatically adjusted to a preset amount. Further, in Japanese Patent Laid-Open No. 5-317660,
An apparatus is disclosed which uses a plurality of membrane separators and adjusts the backwash interval based on the detected raw water turbidity.
【０００４】[0004]
【発明が解決しようとする課題】しかし、前記特開平４
−２４７２２６号公報記載の方法では、目的とする透過
水量に達したか否かを確認するために透過水量自体を測
定することとしているため、調節ならびに確認に長時間
を要する。また、特開平５−３１７６６０号公報記載の
装置では、原水濁度を検知し透過速度を低下させずに安
定させるよう改善された膜分離装置であるが、その制御
は洗浄間隔のみの調節にとどまる。However, the above-mentioned Japanese Unexamined Patent Application Publication No.
In the method described in Japanese Patent No. 247226, the permeated water amount itself is measured in order to confirm whether or not the target permeated water amount has been reached, and therefore, it takes a long time for adjustment and confirmation. Further, the device described in Japanese Patent Laid-Open No. 5-317660 is an improved membrane separation device that detects the turbidity of raw water and stabilizes it without lowering the permeation rate, but the control is limited to adjustment of only the cleaning interval. .
【０００５】一方、中空糸膜モジュールを使用した水浄
化システムにおいては、透過水量を一定に保つことは、
水浄化システムの安定した運行の確保、最終目的物たる
透過水量の安定確保のみならず、中空糸膜モジュールの
寿命にも影響を及ぼすものと考えられる。すなわち、一
旦目詰まりを発生させた中空糸膜はその洗浄が容易では
ないことから、目詰まりを防止して一定した膜状態を維
持させることは、中空糸膜の膜状態の安定化につなが
り、中空糸膜モジュールの延命にも貢献すると考えられ
るからである。このため水浄化システムにおける透過水
量を、中空糸膜の膜状態の指標ととらえ、この透過水量
を一定値に維持させる水浄化システムの運転は、かかる
目的の達成のために極めて重要である。このような現状
のもと、従来の設備をそのまま使用することができ、し
かも迅速な透過水量の調節が可能であり、その調節の方
法も適宜選択が可能な水処理システムの運転方法の開発
が強く求められる。On the other hand, in a water purification system using a hollow fiber membrane module, it is necessary to keep the amount of permeated water constant.
It is considered that not only ensuring stable operation of the water purification system and ensuring stable amount of permeated water as the final target, but also affecting the life of the hollow fiber membrane module. That is, since the hollow fiber membrane that has once been clogged is not easy to clean, preventing clogging and maintaining a constant membrane state leads to stabilization of the membrane state of the hollow fiber membrane, This is because it is believed that it will also contribute to the life extension of the hollow fiber membrane module. Therefore, the amount of permeated water in the water purification system is regarded as an index of the membrane state of the hollow fiber membrane, and the operation of the water purification system for maintaining this amount of permeated water at a constant value is extremely important for achieving such an object. Under these circumstances, conventional equipment can be used as it is, and the amount of permeated water can be adjusted quickly, and the method for adjusting the water treatment system can be appropriately selected. Strongly demanded.
【０００６】[0006]
【課題を解決するための手段】このような現状に鑑み、
本発明者らは原水濁度と透過水量ならびに回収率の関係
を詳細に検討した結果、これらに特定の関係式が成立す
ることを見いだし、この特定式に基づき回収率を制御す
ることにより透過水量を一定値に維持できることに基づ
き、本発明を完成するに至った。[Means for Solving the Problems] In view of such a current situation,
As a result of detailed examination of the relationship between the raw water turbidity, the amount of permeated water, and the recovery rate, the inventors found that a specific relational expression holds for these, and the amount of permeated water can be controlled by controlling the recovery rate based on this specific expression. The present invention has been completed based on the fact that can be maintained at a constant value.
【０００７】すなわち本発明は、逆洗を含むクロスフロ
ー濾過による中空糸膜モジュールを用いた水浄化システ
ムにおいて、回収率を次式（１）に従って制御すること
を特徴とする水浄化システムの運転方法を提供するもの
である。That is, according to the present invention, in a water purification system using a hollow fiber membrane module by cross-flow filtration including backwashing, the recovery rate is controlled according to the following equation (1). Is provided.
【０００８】[0008]
【数３】 (Equation 3)
【０００９】また、前記制御が逆流洗浄によることを特
徴とする水浄化システムの運転方法を提供するものであ
る。さらに、前記中空糸膜モジュールの膜材質が酢酸セ
ルロースであることを特徴とする水浄化システムの運転
方法を提供するものである。さらに、これらの逆洗水
が、膜洗浄剤を併用することを特徴とする水浄化システ
ムの連続運転方法を提供するものである。加えて、濁度
と、制御前回収率Ｒ0とから上記式（１）で示す回収率
Ｒを演算する演算制御装置を有することを特徴とするク
ロスフロー濾過による中空糸膜モジュールを用いた水浄
化装置を提供するものである。以下、本発明を詳細に説
明する。Further, the present invention provides a method for operating a water purification system, wherein the control is by backwashing. Further, the present invention provides a method for operating a water purification system, wherein the membrane material of the hollow fiber membrane module is cellulose acetate. Furthermore, these backwash waters provide a continuous operation method of a water purification system characterized by using a membrane cleaning agent together. In addition, water using a hollow fiber membrane module by cross-flow filtration, characterized in that it has a calculation control device that calculates the recovery rate R shown in the above formula (1) from the turbidity and the previous control yield R 0. A purification device is provided. Hereinafter, the present invention will be described in detail.
【００１０】本発明における水浄化システムの運転方法
は、原水濁度を指標として次式（１）に基づいて回収率
を調節することにより透過水量を一定値に維持するもの
である。The operation method of the water purification system in the present invention is to maintain the permeated water amount at a constant value by adjusting the recovery rate based on the following equation (1) using the raw water turbidity as an index.
【００１１】[0011]
【数４】 [Equation 4]
【００１２】式中、設定透過水量Ｊ値は、水浄化システ
ムの運転の目的とする透過水量として任意に設定する値
であり、０．０２〜０．１５ｍ3／ｍ2・ｈｒの範囲、特
には０．０５〜０．１０ｍ3／ｍ2・ｈｒの範囲であるこ
とが好ましい。この範囲であれば水浄化システムの運転
効率を低下させることなく、また中空糸膜に過度の負担
を掛けることもない。In the equation, the set permeated water amount J value is a value arbitrarily set as the permeated water amount for the purpose of operating the water purification system, and is in the range of 0.02 to 0.15 m 3 / m 2 · hr, especially Is preferably in the range of 0.05 to 0.10 m 3 / m 2 · hr. Within this range, the operating efficiency of the water purification system is not reduced and the hollow fiber membrane is not overloaded.
【００１３】式中、定数ｋ値は膜モジュールのサイズに
より相違するが、水浄化システムの通常使用において膜
モジュールの素材、原水温度、逆洗条件によらない特定
値を選択でき、好ましくは１０〜４０の範囲、さらに好
ましくは２０〜３０の範囲である。In the formula, the constant k value varies depending on the size of the membrane module, but in normal use of the water purification system, a specific value which does not depend on the material of the membrane module, the raw water temperature, and the backwashing condition can be selected, and preferably 10 to 10. It is in the range of 40, more preferably in the range of 20-30.
【００１４】式中、定数Ａ値は膜モジュールの素材、原
水温度、回収率により相違するが、温度０〜５０℃、回
収率７５〜９９％の範囲では、０．０１〜０．２０ｍ3
／ｍ2・ｈｒの範囲、特には０．０５〜０．１５ｍ3／ｍ
2・ｈｒの範囲であればよく、使用する膜モジュール、
原水による予試験により選択することができる。なお、
水浄化システムの運転において必要に応じて適宜Ａ値の
温度補正、回収率補正を実施してもよい。In the formula, the constant A value varies depending on the material of the membrane module, the raw water temperature, and the recovery rate, but 0.01 to 0.20 m 3 in the temperature range of 0 to 50 ° C. and the recovery rate of 75 to 99%.
/ M 2 · hr, especially 0.05 to 0.15 m 3 / m
It should be in the range of 2 · hr, the membrane module used,
It can be selected by a preliminary test with raw water. In addition,
In the operation of the water purification system, the temperature A value and the recovery rate may be appropriately corrected as necessary.
【００１５】式中、定数Ｂ値は好ましくは０．０２〜
０．０５ｍ3／ｍ2・ｈｒの範囲であれば、水浄化システ
ムの通常使用において原水温度、回収率、膜モジュール
の素材等によらず特定値を選択することができる。な
お、式中の濁度Ｔ値は、濁度計により測定した原水の濁
度である。また、式中の制御前回収率Ｒ0とは、原水濁
度の変化により回収率を調節する前の回収率をいい、系
外排出された濁質物質を含む排出液量の原水供給量に対
する割合（（透過水量−逆洗水量）／透過水量）で示さ
れる。In the formula, the constant B value is preferably 0.02 to
Within the range of 0.05 m 3 / m 2 · hr, a specific value can be selected irrespective of the raw water temperature, the recovery rate, the material of the membrane module, etc. in the normal use of the water purification system. The turbidity T value in the formula is the turbidity of raw water measured by a turbidimeter. In addition, the control previous yield R 0 in the formula means the recovery rate before the recovery rate is adjusted by the change of the turbidity of the raw water, and is the amount of the discharged liquid containing the suspended matter discharged from the system to the raw water supply amount. It is shown by a ratio ((amount of permeated water-amount of backwash water) / amount of permeated water).
【００１６】本発明による運転方法は、クロスフロー濾
過による中空糸膜モジュールを用いた水浄化システムを
対象とし、中空糸膜モジュールとしては限外濾過膜、精
密濾過膜などを用いることができる。また、クロスフロ
ー濾過方式としては中空糸膜の内側に原水を流入させる
内圧方式が好ましい。さらにその膜材質としては親水性
高分子材料であるポリビニルアルコール、ポリアクリロ
ニトリル共重合体、酢酸セルロースなどが利用でき、特
に酢酸セルロ−スが最適である。The operation method according to the present invention is intended for a water purification system using a hollow fiber membrane module by cross-flow filtration, and as the hollow fiber membrane module, an ultrafiltration membrane, a microfiltration membrane or the like can be used. Further, as the cross-flow filtration method, an internal pressure method in which raw water is allowed to flow inside the hollow fiber membrane is preferable. Further, as the material of the film, polyvinyl alcohol, polyacrylonitrile copolymer, cellulose acetate and the like which are hydrophilic polymer materials can be used, and cellulose acetate is most suitable.
【００１７】浄化用に供給される原水としては地下水、
雨水、河川水および湖沼水などの天然水を用いることが
できる。The raw water supplied for purification is groundwater,
Natural water such as rainwater, river water and lake water can be used.
【００１８】[0018]
【実施例】本発明による逆洗を含むクロスフロー濾過に
よる水浄化システムの運転方法の一例を図１を用いて説
明するが、本発明はこれに限定されるものではない。EXAMPLE An example of the method of operating the water purification system by cross-flow filtration including backwash according to the present invention will be described with reference to FIG. 1, but the present invention is not limited to this.
【００１９】まず水浄化システムの運転はクロスフロー
濾過による透過水生成と、中空糸膜モジュールの目詰ま
りを防ぐための逆洗とを交互に実施する。用いた中空糸
膜モジュールは酢酸セルロース膜であり、Ａ＝０．１２
ｍ3／ｍ2・ｈｒ、Ｂ＝０．０３５ｍ3／ｍ2・ｈｒ、ｋ＝
２０として算出式を設定した。原水濁度は濁度計でモニ
ターし、制御前回収率は系外に排出された濁質成分を含
む排出液量から算出し、水浄化システムの設定透過水量
は２ｍ3／ｍ2・ｈｒと設定した。First, in the operation of the water purification system, generation of permeated water by crossflow filtration and backwashing for preventing clogging of the hollow fiber membrane module are alternately carried out. The hollow fiber membrane module used is a cellulose acetate membrane, A = 0.12
m 3 / m 2 · hr, B = 0.035 m 3 / m 2 · hr, k =
The calculation formula was set as 20. The raw water turbidity is monitored by a turbidimeter, and the previous control yield is calculated from the amount of effluent containing turbid components discharged outside the system, and the set permeated water amount of the water purification system is 2 m 3 / m 2 · hr. Set.
【００２０】水浄化システム運転時のクロスフロー濾過
時と逆洗時におけるポンプ、流路弁の操作は以下の通り
である。まず、クロスフロー濾過においては透過水自動
弁１３を開、洗浄水排出自動弁１４、逆洗自動弁１９は
閉の状態でポンプ１１により原水を中空糸膜モジュール
に供給して濾過を行い、生成した透過水をタンク１７に
貯留する。なお、中空糸膜モジュールを透過しない原水
はライン１６、ポンプ１１を経て再び中空糸膜モジュー
ル１２に送られる。一方逆洗においては、中空糸膜モジ
ュールの原水側内面に付着した濁質成分を除去するため
に、透過水生成時とは逆方向に中空糸膜モジュールに透
過水を供給し、膜面に付着した濁質成分を剥離したの
ち、濁質成分を系外へ排出する。中空糸膜モジュールの
逆洗は、３０分から５時間に一度程度の頻度で、透過水
自動弁１３を閉、洗浄水排出自動弁１４、逆洗自動弁１
９を開とすると共に、ポンプ１８により透過水タンク１
７の透過水の一部を透過水生成時とは逆方向に中空糸膜
モジュール１２に供給する。これにより中空糸膜モジュ
ールの原水供給側内面の濁質成分を剥離したのち、濁質
成分を高濃度に含有した洗浄水をライン１５を経て洗浄
水排出自動弁１４から系外へ排出させる。ここに制御前
回収率は洗浄水排出自動弁１４から排出される排水液量
に基づいて算出される。なお、逆洗時には、ポンプ１１
を停止させ、原水の供給を停止する。The operation of the pump and the flow path valve at the time of cross-flow filtration and backwashing during the operation of the water purification system are as follows. First, in cross-flow filtration, the permeated water automatic valve 13 is opened, the wash water discharge automatic valve 14 and the backwash automatic valve 19 are closed, and raw water is supplied to the hollow fiber membrane module by the pump 11 to perform filtration to generate it. The permeated water is stored in the tank 17. The raw water that does not pass through the hollow fiber membrane module is sent to the hollow fiber membrane module 12 again via the line 16 and the pump 11. On the other hand, in backwashing, in order to remove turbidity components adhering to the raw water side inner surface of the hollow fiber membrane module, permeated water is supplied to the hollow fiber membrane module in the direction opposite to that at the time of permeated water generation, and adheres to the membrane surface. After removing the suspended components, the suspended components are discharged out of the system. The backwashing of the hollow fiber membrane module is performed once every 30 minutes to 5 hours, with the permeated water automatic valve 13 being closed, the wash water discharge automatic valve 14 and the backwash automatic valve 1 being used.
9 is opened and the permeate tank 1 is pumped by the pump 18.
A part of the permeated water of No. 7 is supplied to the hollow fiber membrane module 12 in the direction opposite to that at the time of generating the permeated water. As a result, the suspended components on the inner surface of the hollow fiber membrane module on the raw water supply side are peeled off, and then the cleaning water containing the suspended components at a high concentration is discharged from the automatic cleaning water discharge valve 14 to the outside of the system through the line 15. Here, the control previous yield is calculated based on the amount of drainage liquid discharged from the automatic wash water discharge valve 14. When backwashing, the pump 11
To stop the supply of raw water.
【００２１】水浄化システムの透過水量を前記設定値２
ｍ3／ｍ2・ｈｒとするため、原水濁度Ｔの変動に基づい
て算出式（１）により得られた回収率Ｒで水浄化システ
ムを操作する。回収率の制御方法としては、逆洗頻度、
逆洗時間、逆洗圧、濾過圧の調節等により実施すること
ができ、これらを適宜組み合わせることも可能である。
例えば逆洗頻度で調節するためには、ポンプ１８を用い
た逆洗間隔の調整ならびにポンプ１８に対応したこられ
自動弁の調整を行う。また、逆洗時間、逆洗圧の調節に
は、ポンプ１８の運転時間ならび吐出圧力を調節するこ
とにより行う。また、濾過圧の調節により回収率の調節
を実施する場合には、原水供給圧の調節を行うこともで
きる。The permeated water amount of the water purification system is set to the set value 2
In order to set m 3 / m 2 · hr, the water purification system is operated with the recovery rate R obtained by the calculation formula (1) based on the fluctuation of the raw water turbidity T. As a control method of the recovery rate, backwash frequency,
It can be carried out by adjusting the backwashing time, the backwashing pressure, the filtration pressure and the like, and it is also possible to appropriately combine these.
For example, in order to adjust the backwashing frequency, the backwashing interval is adjusted using the pump 18 and the automatic drain valve corresponding to the pump 18 is adjusted. The backwash time and backwash pressure are adjusted by adjusting the operating time of the pump 18 and the discharge pressure. Further, when the recovery rate is adjusted by adjusting the filtration pressure, the raw water supply pressure can be adjusted.
【００２２】本発明においては、逆洗において、逆洗水
に膜洗浄剤、酸化剤、酸、塩基性化合物および界面活性
剤などの薬剤の添加が可能である。逆洗時に添加できる
薬剤としては、次亜塩素酸ナトリウム、塩素、過酸化水
素およびオゾンなどの酸化性殺菌剤、クエン酸およびシ
ュウ酸などの有機酸、塩酸および硝酸などの無機酸、水
酸化ナトリウムなどのアルカリおよびカチオン系、ノニ
オン系および両性界面活性剤などがある。透過水に膜洗
浄剤等の薬剤を併用する場合には自動弁１９およびポン
プ１８の設定に加え薬剤ポンプ２２を運転し、薬注自動
弁２５を開とし逆洗を実行する。中空糸膜モジュールは
一般細菌を濾別するが、供給水側に残留した細菌は時間
の経過と共に、中空糸膜モジュール流出口に蓄積した濁
質成分あるいは中空糸膜モジュールなどに付着し繁殖す
る可能性がある。前記膜洗浄剤は、殺菌効果とともに膜
面付着物の分解・洗浄効果も有するため、逆洗効果を上
昇させることができる。In the present invention, in backwashing, it is possible to add agents such as a membrane cleaning agent, an oxidizing agent, an acid, a basic compound and a surfactant to the backwashing water. Agents that can be added during backwashing include sodium hypochlorite, oxidative germicides such as chlorine, hydrogen peroxide and ozone, organic acids such as citric acid and oxalic acid, inorganic acids such as hydrochloric acid and nitric acid, and sodium hydroxide. Such as alkali and cationic, nonionic and amphoteric surfactants. When a chemical such as a membrane cleaning agent is used in combination with the permeated water, the chemical pump 22 is operated in addition to the settings of the automatic valve 19 and the pump 18, and the chemical injection automatic valve 25 is opened to perform backwash. The hollow fiber membrane module filters out general bacteria, but the bacteria remaining on the feed water side can adhere to the turbid components accumulated at the outlet of the hollow fiber membrane module or the hollow fiber membrane module and propagate with time. There is a nature. Since the membrane cleaning agent has a sterilizing effect and a decomposing / cleaning effect on the film surface, the backwashing effect can be increased.
【００２３】本発明においては一定の設定透過水量Ｊに
保つために、原水濁度Ｔと制御前回収率Ｒ0をモニター
することにより回収率Ｒを自動制御することも可能であ
る。例えば図１に示すように、原水濁度の情報から回収
率を演算する演算制御装置２６を設置し、ここから鎖線
で示す制御信号ケーブルにより送られる制御信号によ
り、ポンプ１１、逆洗自動弁１９、ポンプ１８、薬注ポ
ンプ２２および薬注自動弁２５などの自動的に制御が可
能となる。In the present invention, in order to maintain a constant set permeated water amount J, it is possible to automatically control the recovery rate R by monitoring the raw water turbidity T and the control previous yield R 0 . For example, as shown in FIG. 1, an arithmetic and control unit 26 for calculating the recovery rate from the information on the turbidity of raw water is installed, and the pump 11 and the automatic backwash valve 19 are controlled by a control signal sent from a control signal cable shown by a chain line. , 18, the chemical injection pump 22, the automatic chemical injection valve 25, and the like can be automatically controlled.
【００２４】[0024]
【発明の効果】本発明の運転方法によれば、逆洗を含む
中空糸膜モジュールを用いた水浄化システムにおいて、
原水濁度から水浄化システムの回収率を制御するため少
ない情報量で一定の透過水量を維持する水浄化システム
の運転ができる。これにより水浄化システムの安定した
運行の確保、最終目的物たる透過水量の安定確保を図る
ことができる。しかも、中空糸膜の状態を一定に保つこ
とにもつながるため中空糸膜モジュールの延命にも役立
つ。本発明の水浄化システムの運転方法によれば迅速な
透過水量の調節が可能であり、その調節の方法も適宜選
択が可能である。According to the operating method of the present invention, in a water purification system using a hollow fiber membrane module including backwashing,
Since the recovery rate of the water purification system is controlled from the raw water turbidity, it is possible to operate the water purification system that maintains a constant amount of permeated water with a small amount of information. As a result, it is possible to secure stable operation of the water purification system and secure a stable amount of permeated water as the final target. Moreover, it also helps to keep the state of the hollow fiber membrane constant, which is useful for extending the life of the hollow fiber membrane module. According to the method of operating the water purification system of the present invention, the amount of permeated water can be adjusted quickly, and the adjusting method can be appropriately selected.
【図１】 中空糸膜モジュールを用いた水浄化システム
を示す。FIG. 1 shows a water purification system using a hollow fiber membrane module.
１０、２３ 逆止弁 １１、１８ ポンプ １２ 中空糸膜モジュール １３ 透過水自動弁 １４ 濃縮水排出自動弁 １７ 透過水タンク １９ 逆洗自動弁 ２１ 薬剤タンク ２２ 薬注ポンプ ２４ 薬剤注入経路 ２５ 薬注自動弁 ２６ 演算制御装置 10, 23 Check valve 11, 18 Pump 12 Hollow fiber membrane module 13 Permeate water automatic valve 14 Concentrated water discharge automatic valve 17 Permeate water tank 19 Backwash automatic valve 21 Chemical tank 22 Chemical injection pump 24 Chemical injection route 25 Chemical injection automatic Valve 26 Arithmetic control device
Claims (5)
糸膜モジュールを用いた水浄化システムにおいて、回収
率を次式（１）に従って制御することを特徴とする水浄
化システムの運転方法。 【数１】 1. A method of operating a water purification system, characterized in that in a water purification system using a hollow fiber membrane module by cross-flow filtration including backwashing, the recovery rate is controlled according to the following equation (1). [Equation 1]
更によることを特徴とする水浄化システムの運転方法。2. A method of operating a water purification system, wherein the control according to claim 1 is performed by changing a backwashing condition.
ールの膜材質が酢酸セルロースであることを特徴とする
水浄化システムの運転方法。3. A method for operating a water purification system, wherein the membrane material of the hollow fiber membrane module according to claim 1 or 2 is cellulose acetate.
が、膜洗浄剤を併用するものであることを特徴とする水
浄化システムの運転方法。4. A method for operating a water purification system, wherein the backwash water according to any one of claims 1 to 3 uses a membrane cleaning agent together.
（１）で示す回収率Ｒを演算する演算制御装置を有する
ことを特徴とするクロスフロー濾過による中空糸膜モジ
ュールを用いた水浄化装置。 【数２】 5. A hollow fiber membrane module by cross-flow filtration, comprising a calculation control device for calculating a recovery rate R represented by the following formula (1) from raw water turbidity and control previous yield R 0 . The water purification device that was. [Equation 2]
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15789394A JP3514825B2 (en) | 1994-06-16 | 1994-06-16 | Operation method of water purification system and water purification device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP15789394A JP3514825B2 (en) | 1994-06-16 | 1994-06-16 | Operation method of water purification system and water purification device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH081158A true JPH081158A (en) | 1996-01-09 |
| JP3514825B2 JP3514825B2 (en) | 2004-03-31 |
Family
ID=15659726
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP15789394A Expired - Fee Related JP3514825B2 (en) | 1994-06-16 | 1994-06-16 | Operation method of water purification system and water purification device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3514825B2 (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0824857A (en) * | 1994-07-13 | 1996-01-30 | Daicel Chem Ind Ltd | Water purifying apparatus and operation thereof |
| JPH0839065A (en) * | 1994-08-01 | 1996-02-13 | Toshiba Joho Seigyo Syst Kk | Operation control device of water making plant |
| JP2000093753A (en) * | 1998-07-22 | 2000-04-04 | Toray Ind Inc | Method for operating filter membrane module device and filter membrane module device |
| JP2000140585A (en) * | 1998-09-02 | 2000-05-23 | Toray Ind Inc | Operation of membrane separation apparatus, and membrane separation apparatus |
| JP2001070763A (en) * | 1999-09-08 | 2001-03-21 | Asahi Kasei Corp | Membrane washing method |
| JP2005270934A (en) * | 2004-03-26 | 2005-10-06 | Ebara Corp | Membrane filtration method and apparatus |
| JP2006272218A (en) * | 2005-03-30 | 2006-10-12 | Toray Ind Inc | Two-stage membrane filtration system and operation method of two-stage membrane filtration system |
| JP2007152271A (en) * | 2005-12-07 | 2007-06-21 | Kobelco Eco-Solutions Co Ltd | Water treatment system and its operation method |
| JP2018065120A (en) * | 2016-10-21 | 2018-04-26 | 株式会社日立製作所 | Water treatment apparatus and its method |
-
1994
- 1994-06-16 JP JP15789394A patent/JP3514825B2/en not_active Expired - Fee Related
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0824857A (en) * | 1994-07-13 | 1996-01-30 | Daicel Chem Ind Ltd | Water purifying apparatus and operation thereof |
| JPH0839065A (en) * | 1994-08-01 | 1996-02-13 | Toshiba Joho Seigyo Syst Kk | Operation control device of water making plant |
| JP2000093753A (en) * | 1998-07-22 | 2000-04-04 | Toray Ind Inc | Method for operating filter membrane module device and filter membrane module device |
| JP2000140585A (en) * | 1998-09-02 | 2000-05-23 | Toray Ind Inc | Operation of membrane separation apparatus, and membrane separation apparatus |
| JP2001070763A (en) * | 1999-09-08 | 2001-03-21 | Asahi Kasei Corp | Membrane washing method |
| JP2005270934A (en) * | 2004-03-26 | 2005-10-06 | Ebara Corp | Membrane filtration method and apparatus |
| JP2006272218A (en) * | 2005-03-30 | 2006-10-12 | Toray Ind Inc | Two-stage membrane filtration system and operation method of two-stage membrane filtration system |
| JP2007152271A (en) * | 2005-12-07 | 2007-06-21 | Kobelco Eco-Solutions Co Ltd | Water treatment system and its operation method |
| JP2018065120A (en) * | 2016-10-21 | 2018-04-26 | 株式会社日立製作所 | Water treatment apparatus and its method |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3514825B2 (en) | 2004-03-31 |
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