JP2003126855A - Membrane filter system - Google Patents

Membrane filter system

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Publication number
JP2003126855A
JP2003126855A JP2001329474A JP2001329474A JP2003126855A JP 2003126855 A JP2003126855 A JP 2003126855A JP 2001329474 A JP2001329474 A JP 2001329474A JP 2001329474 A JP2001329474 A JP 2001329474A JP 2003126855 A JP2003126855 A JP 2003126855A
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JP
Japan
Prior art keywords
membrane
membrane filtration
raw water
flow rate
water
Prior art date
Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
Pending
Application number
JP2001329474A
Other languages
Japanese (ja)
Inventor
Seiichi Murayama
清一 村山
Masao Kaneko
政雄 金子
Kyotaro Iyasu
巨太郎 居安
Kenji Takeuchi
賢治 竹内
Hitoshi Kawamichi
等 川路
Shoji Uchida
祥司 内田
Mikio Kanemoto
幹男 金元
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Toshiba Corp
Original Assignee
Toshiba Corp
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Toshiba Corp filed Critical Toshiba Corp
Priority to JP2001329474A priority Critical patent/JP2003126855A/en
Publication of JP2003126855A publication Critical patent/JP2003126855A/en
Pending legal-status Critical Current

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  • Investigating, Analyzing Materials By Fluorescence Or Luminescence (AREA)
  • Investigating Or Analysing Materials By Optical Means (AREA)
  • Separation Using Semi-Permeable Membranes (AREA)

Abstract

PROBLEM TO BE SOLVED: To reduce the frequency for physical cleaning, chemical cleaning and replacement of a membrane filter by optimizing the flow rate for treatment according to the water quality and suppressing increase of the pressure difference between membranes, even the water quality of source water varies depending on the season. SOLUTION: The fluorescence intensity of source water 2 is measured by the use of fluorescence analyzer 9. Based on the measured results, a target value of the water volume to be filtered through the membrane is obtained according to the fluorescence intensity of source water 2 making a calculating device 5 for the target value of the water volume to be filtered through the membrane to perform the necessary calculation referring to the target-value/ source-water-fluorescence-intensity table 14. Based on the target value thereof, a flow-rate constant control unit 6 is made to control a flow-rate regulating unit 4, and a membrane module 10 is made to perform the membrane filter treatment of the source water 2 so that the volume of water to be treated by the membrane module 10 and the target value for the water volume to be filtered through the film are in agreement.

Description

【発明の詳細な説明】Detailed Description of the Invention

【０００１】[0001]

【発明の属する技術分野】本発明は、浄水処理、下水処
理、産業排水処理、食品排水処理などで利用される膜濾
過システムに係わり、特に処理対象となる原水の水質な
どに応じて、濾過水量、濾過膜の洗浄周期を最適化する
膜濾過システムに関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a membrane filtration system used in water purification treatment, sewage treatment, industrial wastewater treatment, food wastewater treatment and the like, and particularly, the amount of filtered water depending on the quality of raw water to be treated. , A membrane filtration system for optimizing the cleaning cycle of a filtration membrane.

【０００２】[0002]

【従来の技術】浄水場では、地下水や表流水などを原水
として、着水井に導入し、凝集剤を添加して、フロック
を形成し、沈殿処理を実施する。その後、上澄液を砂濾
過に通して、懸濁物を除去し、最後に消毒用の塩素処理
を施し、需要家に供給している。2. Description of the Related Art In a water purification plant, groundwater, surface water, etc. are used as raw water and introduced into a landing well, a flocculant is added to form flocs, and a precipitation treatment is carried out. After that, the supernatant is passed through a sand filter to remove the suspended matter, and finally subjected to chlorine treatment for disinfection and supplied to customers.

【０００３】この際、凝集沈殿処理工程、砂濾過工程に
より、原水中の濁質成分を除去することができるもの
の、運転管理が難しく、処理水質を一定に確保するのに
多大な労力をかけている。At this time, although the turbidity components in the raw water can be removed by the coagulation-sedimentation process and the sand filtration process, operation management is difficult and a great deal of labor is required to maintain a constant quality of the treated water. There is.

【０００４】近年、膜濾過技術に関する研究開発が進
み、凝集沈殿処理の代わりに、膜濾過処理を導入する自
治体も出てきた。膜濾過処理では、確実に濁質物を除去
できるため、良質な処理水質を確実に得られるという利
点があるが、膜濾過処理により、目詰まりが生じて、膜
間差圧が上昇し、濾過膜に過大な負荷をかけてしまう恐
れがある。In recent years, research and development relating to the membrane filtration technology has progressed, and some local governments have introduced the membrane filtration treatment instead of the coagulation sedimentation treatment. Membrane filtration treatment has the advantage of being able to reliably obtain good quality treated water because it can reliably remove suspended matter, but the membrane filtration treatment causes clogging, increasing the transmembrane pressure difference, and May put an excessive load on the.

【０００５】そこで、このよう濾過膜を使用した膜濾過
システムでは、予め設定された周期で、物理洗浄となる
逆圧洗浄シーケンスを自動起動し、濾過水を透過側から
流す逆圧洗浄を行わせ、膜表面あるいは膜内部の付着物
のうち、可逆的なものを除去し、濾過膜に過大な負荷が
かからないようにしている。Therefore, in the membrane filtration system using the filtration membrane as described above, a back pressure washing sequence, which is physical washing, is automatically started at a preset cycle to perform back pressure washing in which filtered water is passed from the permeate side. Of the deposits on the membrane surface or inside the membrane, reversible substances are removed so that the filter membrane is not overloaded.

【０００６】そして、濾過膜の内部などに、このような
逆圧洗浄で除去できない付着物が蓄積され、膜間差圧が
予め設定されている上限値を越えた時点で、膜濾過処理
を停止して、薬品洗浄を行わせ、物理洗浄で除去できな
かった付着物を除去している。Then, when the deposits that cannot be removed by such back pressure cleaning are accumulated inside the filtration membrane and the transmembrane pressure difference exceeds the preset upper limit value, the membrane filtration process is stopped. Then, chemical cleaning is performed to remove the deposits that could not be removed by physical cleaning.

【０００７】[0007]

【発明が解決しようとする課題】ところで、このような
膜濾過システムでは、物理洗浄を繰り返しながら、膜間
差圧がある程度、高くなったとき、薬品洗浄を実施する
という洗浄サイクルを繰り返し、同じ濾過膜をできるだ
け長く使用するようにしている。By the way, in such a membrane filtration system, while repeating the physical washing, when the transmembrane pressure difference becomes high to some extent, a washing cycle of carrying out chemical washing is repeated to obtain the same filtration. I try to use the membrane as long as possible.

【０００８】そして、薬品洗浄を行っても、濾過膜内部
などの付着物が取り除けなくなり、膜間差圧が予め設定
されている上限値を越えたままになったとき、濾過膜が
劣化したと判断して、濾過膜の交換作業を行わせてい
る。[0008] Then, even if chemical cleaning is performed, it becomes impossible to remove the deposits inside the filtration membrane, and when the transmembrane pressure difference remains above the preset upper limit value, the filtration membrane deteriorates. Judgment is made to replace the filtration membrane.

【０００９】この際、薬品洗浄、濾過膜の交換などを行
わせる毎に、膜濾過処理を停止しなければならないこと
から、このような薬品洗浄の回数、濾過膜の交換回数を
なるべく少なくして、膜濾過システムの運転コストを低
減し、膜濾過システムの稼働率を高くすることが強く望
まれている。At this time, the membrane filtration process must be stopped every time chemical cleaning, replacement of the filtration membrane or the like is performed. Therefore, the number of such chemical cleaning and the number of exchanges of the filtration membrane should be minimized. It is strongly desired to reduce the operating cost of the membrane filtration system and increase the operating rate of the membrane filtration system.

【００１０】本発明は上記の事情に鑑み、システムの運
転コストを低く抑えすることができるとともに、膜処理
水量を多くして、システム稼働率を高くすることができ
る膜濾過システムを提供することを目的としている。In view of the above circumstances, the present invention provides a membrane filtration system which can keep the operating cost of the system low, increase the amount of membrane-treated water, and increase the system operating rate. Has an aim.

【００１１】[0011]

【課題を解決するための手段】上記の目的を達成するた
めに本発明は、請求項１では、膜モジュールを使用し
て、原水の水質を改善する膜濾過システムにおいて、原
水蛍光分析計によって、前記膜モジュールに供給される
前記原水の蛍光強度を測定するとともに、この測定結果
に基づき、膜濾過制御装置によって、前記膜モジュール
で膜濾過処理される前記原水の流量を制御する。[Means for Solving the Problems] In order to achieve the above object, the present invention provides, in claim 1, a membrane filtration system for improving the quality of raw water using a membrane module, by a raw water fluorescence spectrometer, The fluorescence intensity of the raw water supplied to the membrane module is measured, and the flow rate of the raw water subjected to the membrane filtration in the membrane module is controlled by the membrane filtration controller based on the measurement result.

【００１２】これにより、原水の有機物濃度に対応した
蛍光強度を指標にして、処理流量を最適化し、これによ
って膜間差圧上昇を抑えつつ、物理洗浄の回数、薬品洗
浄の回数、濾過膜の交換回数を低減して、システムの運
転コストを低く抑えるとともに、膜処理水量を多くし
て、システム稼働率を高くする。Thus, the processing flow rate is optimized by using the fluorescence intensity corresponding to the organic matter concentration of the raw water as an index, thereby suppressing the rise of the transmembrane pressure difference, the number of times of physical washing, the number of times of chemical washing, and the filtration membrane. The number of replacements is reduced to keep the operating cost of the system low, and the amount of membrane-treated water is increased to increase the system operating rate.

【００１３】請求項２では、請求項１に記載の膜濾過シ
ステムにおいて、前記膜濾過制御装置によって、前記膜
モジュールに供給される前記原水の濁度を測定する原水
濁度計の測定結果、前記原水蛍光分析計の測定結果に基
づき、前記膜モジュールで膜濾過処理される前記原水の
流量を制御する。According to a second aspect of the present invention, in the membrane filtration system according to the first aspect, a measurement result of a raw water turbidimeter for measuring the turbidity of the raw water supplied to the membrane module by the membrane filtration controller, The flow rate of the raw water subjected to the membrane filtration treatment in the membrane module is controlled based on the measurement result of the raw water fluorescence analyzer.

【００１４】これにより、原水の有機物濃度に対応した
蛍光強度と、原水の濁度とを指標にして、処理流量を最
適化し、これによって膜間差圧上昇を抑えつつ、物理洗
浄の回数、薬品洗浄の回数、濾過膜の交換回数を低減し
て、システムの運転コストを低く抑えるとともに、膜処
理水量を多くして、システム稼働率を高くする。Thus, the treatment flow rate is optimized by using the fluorescence intensity corresponding to the organic matter concentration of the raw water and the turbidity of the raw water as an index, thereby suppressing the rise of transmembrane pressure difference, the number of times of physical cleaning, chemicals. The number of times of washing and the number of times of replacement of the filtration membrane are reduced to keep the operating cost of the system low, and the amount of membrane-treated water is increased to increase the system operating rate.

【００１５】請求項３では、請求項１、２のいずれかに
記載の膜濾過システムにおいて、前記膜濾過制御装置に
よって、前記膜モジュールから送出される濾過水の蛍光
強度を測定する濾過水蛍光分析計の測定結果、前記原水
蛍光分析計の測定結果に基づき、前記膜モジュールで膜
濾過処理される前記原水の流量を制御する。According to a third aspect of the present invention, in the membrane filtration system according to any one of the first and second aspects, filtered water fluorescence analysis for measuring the fluorescence intensity of the filtered water delivered from the membrane module by the membrane filtration controller. The flow rate of the raw water subjected to the membrane filtration treatment in the membrane module is controlled based on the measurement result of the meter and the measurement result of the raw water fluorescence analyzer.

【００１６】これにより、原水の有機物濃度に対応した
蛍光強度と、濾過水の溶融性有機物濃度に対応した蛍光
強度とを指標にして、処理流量を最適化し、これによっ
て膜間差圧上昇を抑えつつ、物理洗浄の回数、薬品洗浄
の回数、濾過膜の交換回数を低減して、システムの運転
コストを低く抑えるとともに、膜処理水量を多くして、
システム稼働率を高くする。Thus, the treatment flow rate is optimized by using the fluorescence intensity corresponding to the concentration of organic matter in the raw water and the fluorescence intensity corresponding to the concentration of the soluble organic matter in the filtered water as an index, thereby suppressing an increase in transmembrane pressure difference. At the same time, the number of physical cleaning, the number of chemical cleaning, and the number of exchange of the filtration membrane are reduced to keep the operating cost of the system low and increase the amount of membrane-treated water.
Increase system availability.

【００１７】請求項４では、請求項１乃至３のいずれか
に記載の膜濾過システムにおいて、前記膜濾過制御装置
によって、前記濾過水蛍光分析計の測定結果、前記原水
蛍光分析計の測定結果のうち、少なくともいずれか一
方、または組み合わせ内容に基づき、前記膜モジュール
に対する逆洗浄開始時期を制御する。According to a fourth aspect, in the membrane filtration system according to any one of the first to third aspects, the measurement result of the filtered water fluorescence analyzer and the measurement result of the raw water fluorescence analyzer are measured by the membrane filtration controller. Of these, at least one of them or the combination content is used to control the backwash start timing for the membrane module.

【００１８】これにより、原水の有機物濃度に対応した
蛍光強度と、濾過水の溶融性有機物濃度に対応した蛍光
強度とを指標にして、濾過膜に対する逆洗浄の開始時期
を最適化し、これによって膜間差圧上昇を抑えつつ、物
理洗浄の回数、薬品洗浄の回数、濾過膜の交換回数を低
減して、システムの運転コストを低く抑えるとともに、
膜処理水量を多くして、システム稼働率を高くする。Thus, the backwash start timing for the filtration membrane is optimized by using the fluorescence intensity corresponding to the concentration of the organic matter in the raw water and the fluorescence intensity corresponding to the concentration of the soluble organic matter in the filtered water as an index. While suppressing an increase in the differential pressure, the number of physical washes, chemical washes, and the number of filter membrane exchanges is reduced to keep the operating cost of the system low and
Increase the amount of membrane-treated water to increase system availability.

【００１９】請求項５では、請求項１乃至４のいずれか
に記載の膜濾過システムにおいて、前記濾過水蛍光分析
計、前記原水蛍光分析計のうち、少なくともいずれか一
方に、波長“３４０〜３５０ｎｍ”の間にある特定波長
の励起光と、波長“４２０〜４３０ｎｍ”の間にある特
定の蛍光を使用して、前記原水または前記濾過水の蛍光
強度を測定する。According to a fifth aspect, in the membrane filtration system according to any one of the first to fourth aspects, at least one of the filtered water fluorescence analyzer and the raw water fluorescence analyzer has a wavelength of "340 to 350 nm. The fluorescence intensity of the raw water or the filtered water is measured by using the excitation light of the specific wavelength between "" and the specific fluorescence of the wavelength "420 to 430 nm".

【００２０】これにより、原水、濾過水の有機物濃度を
測定するのに最適な波長の励起光、蛍光を使用して、原
水の蛍光強度、または濾過水の蛍光強度を正確に測定
し、これによって処理流量、濾過膜に対する逆洗浄の開
始時期を最適化して、膜間差圧上昇を抑えつつ、物理洗
浄の回数、薬品洗浄の回数、濾過膜の交換回数を低減し
て、システムの運転コストを低く抑えるとともに、膜処
理水量を多くして、システム稼働率を高くする。Thus, the fluorescence intensity of the raw water or the fluorescence intensity of the filtered water can be accurately measured by using the excitation light and the fluorescence having the wavelengths optimal for measuring the organic matter concentration of the raw water and the filtered water. By optimizing the processing flow rate and the start time of backwashing for the filtration membrane, while suppressing the rise in transmembrane pressure difference, the number of physical washes, the number of chemical washes, and the number of times the filter membrane is replaced can be reduced to reduce the system operating cost. In addition to keeping it low, increase the amount of membrane-treated water to increase the system availability.

【００２１】請求項６では、膜モジュールを使用して、
原水の水質を改善する膜濾過システムにおいて、原水吸
光度計によって、前記膜モジュールに供給される前記原
水の吸光度を測定するとともに、この測定結果に基づ
き、膜濾過制御装置によって、前記膜モジュールで膜濾
過処理される前記原水の流量を制御する。In claim 6, the membrane module is used,
In a membrane filtration system for improving the quality of raw water, the raw water absorbance meter measures the absorbance of the raw water supplied to the membrane module, and based on the measurement result, the membrane filtration controller controls the membrane filtration in the membrane module. Control the flow rate of the raw water being treated.

【００２２】これにより、原水の有機物濃度に対応した
吸光度を指標にして、処理流量を最適化し、これによっ
て膜間差圧上昇を抑えつつ、物理洗浄の回数、薬品洗浄
の回数、濾過膜の交換回数を低減して、システムの運転
コストを低く抑えるとともに、膜処理水量を多くして、
システム稼働率を高くする。Thus, the processing flow rate is optimized by using the absorbance corresponding to the concentration of organic matter in the raw water as an index, whereby the number of times of physical cleaning, the number of times of chemical cleaning, and the replacement of the filtration membrane are suppressed while suppressing an increase in transmembrane pressure difference. By reducing the number of times, keeping the operating cost of the system low, and increasing the amount of membrane-treated water,
Increase system availability.

【００２３】請求項７では、請求項６に記載の膜濾過シ
ステムにおいて、前記膜濾過制御装置によって、前記膜
モジュールに供給される前記原水の濁度を測定する原水
濁度計の測定結果、前記原水吸光度計の測定結果に基づ
き、前記膜モジュールで膜濾過処理される前記原水の流
量を制御する。According to a seventh aspect of the present invention, in the membrane filtration system according to the sixth aspect, a measurement result of a raw water turbidimeter for measuring the turbidity of the raw water supplied to the membrane module by the membrane filtration control device, The flow rate of the raw water subjected to membrane filtration in the membrane module is controlled based on the measurement result of the raw water absorbance meter.

【００２４】これにより、原水の有機物濃度に対応した
吸光度と、原水の濁度とを指標にして、処理流量を最適
化し、これによって膜間差圧上昇を抑えつつ、物理洗浄
の回数、薬品洗浄の回数、濾過膜の交換回数を低減し
て、システムの運転コストを低く抑えるとともに、膜処
理水量を多くして、システム稼働率を高くする。Thus, the treatment flow rate is optimized by using the absorbance corresponding to the organic matter concentration of the raw water and the turbidity of the raw water as an index, thereby suppressing the rise of transmembrane pressure difference, the number of physical washings, and chemical washing. The operating cost of the system is kept low by reducing the number of times of filtration and the number of times of exchange of the filtration membrane, and the system operating rate is increased by increasing the amount of membrane-treated water.

【００２５】請求項８では、請求項６、７のいずれかに
記載の膜濾過システムにおいて、前記膜濾過制御装置に
よって、前記膜モジュールから送出される濾過水の吸光
度を測定する濾過水吸光度計の測定結果、前記原水吸光
度計の測定結果に基づき、前記膜モジュールで膜濾過処
理される前記原水の流量を制御する。According to an eighth aspect of the present invention, in the membrane filtration system according to any of the sixth and seventh aspects, a filtered water absorbance meter for measuring the absorbance of the filtered water delivered from the membrane module by the membrane filtration controller. Based on the measurement result and the measurement result of the raw water absorptiometer, the flow rate of the raw water that is subjected to membrane filtration in the membrane module is controlled.

【００２６】これにより、原水の有機物濃度に対応した
吸光度と、濾過水の有機物濃度に対応した吸光度とを指
標にして、処理流量を最適化し、これによって膜間差圧
上昇を抑えつつ、物理洗浄の回数、薬品洗浄の回数、濾
過膜の交換回数を低減して、システムの運転コストを低
く抑えるとともに、膜処理水量を多くして、システム稼
働率を高くする。Thus, the treatment flow rate is optimized by using the absorbance corresponding to the organic matter concentration of the raw water and the absorbance corresponding to the organic matter concentration of the filtered water as an index, thereby suppressing an increase in transmembrane pressure difference and performing physical cleaning. The operating cost of the system is kept low by reducing the number of times, the number of times of chemical cleaning, and the number of times of exchange of the filtration membrane, and the amount of membrane-treated water is increased to increase the system operating rate.

【００２７】請求項９では、請求項６乃至８のいずれか
に記載の膜濾過システムにおいて、前記膜濾過制御装置
によって、前記濾過水吸光度計の測定結果、前記原水吸
光度計の測定結果のうち、少なくともいずれか一方、ま
たは組み合わせ内容に基づき、前記膜モジュールに対す
る逆洗浄開始時期を制御する。According to a ninth aspect of the present invention, in the membrane filtration system according to any of the sixth to eighth aspects, among the measurement results of the filtered water absorptiometer and the raw water absorptiometer by the membrane filtration controller. The backwash start timing for the membrane module is controlled based on at least one or the combination content.

【００２８】これにより、原水の有機物濃度に対応した
吸光度と、濾過水の有機物濃度に対応した吸光度とを指
標にして、濾過膜に対する逆洗浄の開始時期を最適化
し、これによって膜間差圧上昇を抑えつつ、物理洗浄の
回数、薬品洗浄の回数、濾過膜の交換回数を低減して、
システムの運転コストを低く抑えるとともに、膜処理水
量を多くして、システム稼働率を高くする。Thus, the start time of backwashing of the filtration membrane is optimized by using the absorbance corresponding to the organic matter concentration of the raw water and the absorbance corresponding to the organic matter concentration of the filtered water as an index, thereby increasing the transmembrane pressure difference. While reducing the number of physical cleaning, chemical cleaning, and filter membrane replacement,
The system operating cost will be kept low and the amount of membrane treated water will be increased to increase the system operating rate.

【００２９】請求項１０では、請求項６乃至９のいずれ
かに記載の膜濾過システムにおいて、前記濾過水吸光度
計、前記原水吸光度計のうち、少なくともいずれか一方
に、波長“２５０〜２７０ｎｍ”の間にある特定波長の
光に対する吸光度を使用して、前記原水または前記濾過
水の吸光度を測定する。According to a tenth aspect of the present invention, in the membrane filtration system according to any of the sixth to ninth aspects, at least one of the filtered water absorbance meter and the raw water absorbance meter has a wavelength of "250 to 270 nm". The absorbance of the raw water or the filtered water is measured by using the absorbance of light having a specific wavelength in between.

【００３０】これにより、原水、濾過水の有機物濃度を
測定するのに最適な波長の光を使用して、原水の吸光
度、または濾過水の吸光度とを正確に測定し、これによ
って処理流量、濾過膜に対する逆洗浄の開始時期を最適
化して、膜間差圧上昇を抑えつつ、物理洗浄の回数、薬
品洗浄の回数、濾過膜の交換回数を低減して、システム
の運転コストを低く抑えるとともに、膜処理水量を多く
して、システム稼働率を高くする。Accordingly, the absorbance of the raw water or the absorbance of the filtered water is accurately measured by using the light having the optimum wavelength for measuring the organic matter concentration of the raw water and the filtered water. By optimizing the start time of backwashing for the membrane, suppressing the rise of transmembrane pressure difference, reducing the number of times of physical washing, the number of chemical washing, the number of times of replacement of the filtration membrane, and keeping the operating cost of the system low, Increase the amount of membrane-treated water to increase system availability.

【００３１】請求項１１では、請求項６乃至１０のいず
れかに記載の膜濾過システムにおいて、前記濾過水吸光
度計、前記原水吸光度計のうち、少なくともいずれか一
方に、波長“３８０〜４００ｎｍ”の間にある特定波長
の光に対する吸光度を使用して、前記原水または前記濾
過水の吸光度を測定する。In the eleventh aspect, in the membrane filtration system according to any of the sixth to tenth aspects, at least one of the filtered water absorbance meter and the raw water absorbance meter has a wavelength of "380 to 400 nm". The absorbance of the raw water or the filtered water is measured by using the absorbance of light having a specific wavelength in between.

【００３２】これにより、原水、濾過水の有機物濃度う
ち、フミン酸などの濃度を測定するのに最適な波長の光
を使用して、原水の吸光度、または濾過水の吸光度とを
正確に測定し、これによって処理流量、濾過膜に対する
逆洗浄の開始時期を最適化して、膜間差圧上昇を抑えつ
つ、物理洗浄の回数、薬品洗浄の回数、濾過膜の交換回
数を低減して、システムの運転コストを低く抑えるとと
もに、膜処理水量を多くして、システム稼働率を高くす
る。Thus, the absorbance of the raw water or the absorbance of the filtered water can be accurately measured by using the light having the optimum wavelength for measuring the concentration of humic acid or the like among the concentrations of the organic substances in the raw water and the filtered water. By doing this, the processing flow rate and the start time of backwashing for the filtration membrane are optimized, while suppressing the rise of the transmembrane pressure difference, the number of physical washes, the number of chemical washes, and the number of exchanges of the filtration membrane are reduced, and the system While keeping the operating cost low, increase the amount of membrane-treated water to increase the system availability.

【００３３】請求項１２では、請求項１乃至１１のいず
れかに記載の膜濾過システムにおいて、前記膜濾過制御
装置によって、前記膜モジュールに対する逆洗浄処理か
ら排出される洗浄排水の濁度を測定する洗浄排水濁度計
の測定結果、または前記洗浄排水の蛍光強度を測定する
洗浄水蛍光分析計の測定結果、あるいは前記洗浄排水の
吸光度を測定する洗浄水吸光度計の測定結果のいずれか
に基づき、前記膜モジュールに対する逆洗浄終了時期を
制御する。According to a twelfth aspect of the present invention, in the membrane filtration system according to any one of the first to eleventh aspects, the turbidity of the cleaning wastewater discharged from the backwashing process for the membrane module is measured by the membrane filtration controller. Based on the measurement result of the wash drainage turbidimeter, or the measurement result of the wash water fluorescence analyzer that measures the fluorescence intensity of the wash drainage, or the measurement result of the wash water absorbance meter that measures the absorbance of the wash drainage, The end time of backwashing for the membrane module is controlled.

【００３４】これにより、濾過膜を逆洗浄したときに排
出される洗浄排水の濁度を測定して、これによって濾過
膜に対する逆洗浄の終了時期を最適化し、膜間差圧上昇
を抑えつつ、物理洗浄の回数、薬品洗浄の回数、濾過膜
の交換回数を低減して、システムの運転コストを低く抑
えるとともに、膜処理水量を多くして、システム稼働率
を高くする。Thus, the turbidity of the cleaning wastewater discharged when the filter membrane is backwashed is measured, and the end time of the backwashing of the filter membrane is optimized by this, while suppressing the rise of the transmembrane pressure difference. The number of times of physical cleaning, the number of times of chemical cleaning, and the number of times of exchanging the filtration membrane are reduced to reduce the operating cost of the system, increase the amount of membrane-treated water, and increase the system operating rate.

【００３５】[0035]

【発明の実施の形態】《第１実施形態》第１実施形態を
図１を参照して説明する。BEST MODE FOR CARRYING OUT THE INVENTION << First Embodiment >> A first embodiment will be described with reference to FIG.

【００３６】図１に示す膜濾過システム１ａは、処理対
象となる原水２の蛍光強度を測定しつつ、膜濾過処理し
て、原水２中の有機物などを除去する膜濾過装置３と、
膜濾過装置３から送出される濾過水１１の流量を計測し
つつ、指定されたバルブ開度で、濾過水１１を通過し
て、次の処理に送出する処理流量調整装置４と、膜濾過
装置３から出力される蛍光強度検知信号に基づき、膜濾
過水流量目標値を演算する膜濾過水流量目標値演算装置
５と、膜濾過水流量目標値演算装置５から出力される膜
濾過水流量目標値指示信号、処理流量調整装置４から出
力される流量検知信号などに基づき、バルブ開度指定信
号を生成して、処理流量調整装置４の流量を制御する流
量一定制御装置６とを備えている。The membrane filtration system 1a shown in FIG. 1 measures the fluorescence intensity of the raw water 2 to be treated while performing a membrane filtration treatment to remove organic substances and the like in the raw water 2, and
A processing flow rate adjusting device 4 that passes through the filtered water 11 at a designated valve opening and sends it to the next process while measuring the flow rate of the filtered water 11 sent from the membrane filtering device 3, and a membrane filtering device. Membrane filtered water flow rate target value calculation device 5 for calculating the membrane filtered water flow rate target value based on the fluorescence intensity detection signal output from No. 3, and the membranous filtered water flow rate target output from the membrane filtered water flow rate target value calculation device 5. A constant flow controller 6 for controlling the flow rate of the processing flow rate adjusting device 4 by generating a valve opening designating signal based on the value instruction signal, the flow rate detection signal output from the processing flow rate adjusting device 4, and the like. .

【００３７】膜濾過装置３は、前の処理から送水された
原水２に含まれている濁質成分のうち、大きな濁質成分
を取り除く除濁用前処理器７と、除濁用前処理器７から
原水２を取り込む原水ポンプ８と、原水ポンプ８によっ
て取り込まれた原水２に含まれている有機物濃度を測定
するのに最適な波長範囲“３４０〜３５０ｎｍ”内の特
定波長、例えば波長“３４５ｎｍ”の励起光を照射しな
がら、原水２から発せられる蛍光のうち、原水２に含ま
れている有機物濃度を測定するのに最適な波長範囲“４
２０〜４３０ｎｍ”内の特定波長、例えば波長“４２５
ｎｍ”の蛍光を選択して、蛍光強度を測定し、蛍光強度
検知信号を生成する蛍光分析計９と、原水ポンプ８によ
って取り込まれた原水２を膜濾過して、原水２に含まれ
ている有機物などを除去する膜モジュール１０とを備え
ている。The membrane filtration device 3 includes a turbidity pretreatment device 7 for removing large turbidity components out of the turbidity components contained in the raw water 2 sent from the previous treatment, and a turbidity pretreatment device. A raw water pump 8 that takes in the raw water 2 from 7 and a specific wavelength within the optimum wavelength range “340 to 350 nm” for measuring the concentration of organic matter contained in the raw water 2 taken in by the raw water pump 8, for example, the wavelength “345 nm” Of the fluorescence emitted from the raw water 2 while irradiating the excitation light of ", the optimum wavelength range for measuring the concentration of organic substances contained in the raw water 2" 4
A specific wavelength within 20 to 430 nm, for example, the wavelength "425
Fluorescence of 9 nm "is selected, the fluorescence intensity is measured, and the raw water 2 taken in by the raw water pump 8 and the fluorescence analyzer 9 for generating the fluorescence intensity detection signal are contained in the raw water 2 by membrane filtration. The membrane module 10 for removing organic substances and the like is provided.

【００３８】処理流量調整装置４は、バルブの開度を検
知して、バルブ開度検知信号を生成し、これを流量一定
制御装置６に供給しながら、流量一定制御装置６から出
力されるバルブ開度指定信号の値に応じてバルブを開い
て、膜濾過装置３から送出される濾過水１１の通過流量
を調整する流量調整弁１２と、流量調整弁１２から送水
される濾過水１１の流量を測定して、流量検知信号を生
成し、これを流量一定制御装置６に供給しながら、流量
測定済みの濾過水１１を次の処理に送水する濾過水流量
計１３とを備えている。The processing flow rate adjusting device 4 detects the opening degree of the valve, generates a valve opening degree detection signal, supplies the signal to the constant flow rate controlling device 6, and outputs the signal from the constant flow rate controlling device 6. A flow rate adjusting valve 12 that adjusts the passage flow rate of the filtered water 11 sent from the membrane filtering device 3 according to the value of the opening degree designation signal, and a flow rate of the filtered water 11 sent from the flow rate adjusting valve 12. And a filtered water flow meter 13 for sending the filtered water 11 whose flow rate has been measured to the next process while generating a flow rate detection signal and supplying it to the constant flow rate control device 6.

【００３９】また、膜濾過水流量目標値演算装置５は、
膜濾過装置３から出力される蛍光強度検知信号を取り込
むとともに、設計データ、測定データなどによって得ら
れる膜濾過水流量目標値／原水蛍光強度テーブル１４
（図４参照）を参照しながら、前記蛍光強度検知信号で
示される蛍光強度に対応する膜濾過水流量目標値を求め
て、膜濾過水流量目標値指示信号を生成し、これを流量
一定制御装置６に供給する。Further, the membrane filtration water flow rate target value calculation device 5 is
Membrane filtration water flow rate target value / raw water fluorescence intensity table 14 obtained from the design data, measurement data, etc. while taking in the fluorescence intensity detection signal output from the membrane filtration device 3
With reference to FIG. 4, a membrane filtration water flow rate target value corresponding to the fluorescence intensity indicated by the fluorescence intensity detection signal is obtained, a membrane filtration water flow rate target value instruction signal is generated, and this is controlled to a constant flow rate. Supply to the device 6.

【００４０】流量一定制御装置６は、膜濾過水流量目標
値演算装置５から出力される膜濾過水流量目標値指示信
号で示される膜濾過水流量目標値と処理流量調整装置４
から出力される流量検知信号で示される濾過水流量とを
比較し、これらの比較結果と、処理流量調整装置４から
出力されるバルブ開度検知信号で示されるバルブ開度と
に基づき、膜濾過水流量目標値と、濾過水流量とを一致
するのに必要なバルブ開度を求めて、バルブ開度を示す
バルブ開度指定信号を処理流量調整装置４に供給する。The constant flow rate control device 6 includes a membrane filtration water flow rate target value indicated by a membrane filtration water flow rate target value instruction signal output from the membrane filtration water flow rate target value calculation device 5 and a treatment flow rate adjusting device 4.
The filtered water flow rate indicated by the flow rate detection signal output from the filter is compared, and based on the comparison result and the valve opening degree indicated by the valve opening degree detection signal output from the processing flow rate adjusting device 4, the membrane filtration is performed. The valve opening degree required to match the target water flow rate value with the filtered water flow rate is obtained, and a valve opening degree designation signal indicating the valve opening degree is supplied to the processing flow rate adjusting device 4.

【００４１】次に、第１実施形態の動作を説明する。Next, the operation of the first embodiment will be described.

【００４２】まず、膜濾過システム１ａを稼働する前
に、次に述べる手順で、膜濾過水流量目標値／原水蛍光
強度テーブル１４が作成される。First, before operating the membrane filtration system 1a, the membrane filtration water flow rate target value / raw water fluorescence intensity table 14 is created in the following procedure.

【００４３】一般的に、膜モジュール１０を定期的に物
理洗浄しながら、膜モジュール１０に対し、一定処理流
量で、一定水質の原水２を供給し、膜濾過し続けると、
図２の膜濾過時間／膜間差圧グラフに示すように、膜濾
過の経過時間に応じて、膜間差圧が上昇し、予め設定さ
れている薬品洗浄開始膜間差圧値を越える毎に、薬品洗
浄を行わなければならない。Generally, while physically cleaning the membrane module 10 periodically, the raw water 2 having a constant water quality is supplied to the membrane module 10 at a constant treatment flow rate and the membrane filtration is continued.
As shown in the membrane filtration time / membrane pressure difference graph of FIG. 2, the membrane pressure difference increases according to the elapsed time of the membrane filtration, and every time the preset value of the chemical cleaning start membrane pressure difference is exceeded. First, chemical cleaning must be performed.

【００４４】このとき、原水２の流量を“６０Ｌ／ｈｒ
／ｍ２”にしたときに比べて、“４０Ｌ／ｈｒ／ｍ２”
にした方が膜モジュール１０内の濾過膜に負担をかける
ことなく、膜濾過時間を長くして、薬品洗浄回数を低減
することができる。At this time, the flow rate of the raw water 2 is set to "60 L / hr.
/ "Than when you," m 2 40L / hr / m 2 "
It is possible to extend the membrane filtration time and reduce the number of times of chemical cleaning without imposing a burden on the filtration membrane in the membrane module 10.

【００４５】また、膜モジュール１０に供給する原水２
に含まれる有機物が多くなり、原水２を蛍光分析したと
きに得られる蛍光の強度が強くなると、図３の膜間差圧
上昇率／膜濾過水流量グラフに示すように、最大許容差
圧上昇率以下にするのに必要な膜濾過水量が小さくな
る。Further, the raw water 2 supplied to the membrane module 10
When the amount of organic matter contained in the raw water 2 increases and the intensity of the fluorescence obtained when the raw water 2 is subjected to fluorescence analysis increases, the maximum allowable differential pressure rise is shown in the transmembrane pressure increase rate / membrane filtered water flow rate graph of FIG. The amount of membrane-filtered water required to keep the ratio below is reduced.

【００４６】そして、図３に示す差圧上昇率と、図２に
示す膜間差圧の傾き（差圧上昇率）とが対応しているこ
とから、これら図２に示す膜濾過時間／膜間差圧グラフ
と、図３の膜間差圧上昇率／膜濾過水流量グラフとに基
づき、図４に示ように、膜モジュール１０内に設けられ
た濾過膜の最大許容差圧上昇率を越えないようにしなが
ら、薬品洗浄回数を少なくするために必要な膜濾過水流
量目標値／原水蛍光強度テーブル１４が作成され、これ
が膜濾過流量目標値演算装置５に格納される。Since the differential pressure increase rate shown in FIG. 3 and the transmembrane pressure difference gradient (differential pressure increase rate) shown in FIG. 2 correspond to each other, the membrane filtration time / membrane shown in FIG. Based on the differential pressure graph and the transmembrane pressure increase rate / membrane filtered water flow rate graph of FIG. 3, the maximum allowable differential pressure increase rate of the filtration membrane provided in the membrane module 10 is calculated as shown in FIG. A membrane filtration water flow rate target value / raw water fluorescence intensity table 14 required to reduce the number of times of chemical cleaning is created while not exceeding the limit, and this is stored in the membrane filtration flow rate target value calculation device 5.

【００４７】この後、膜濾過システム１ａが稼働状態に
されて、原水ポンプ８がオン状態にされると、除濁用前
処理器７によって、処理対象となる原水２が取り込まれ
て、濁質成分のうち、大きな濁質成分が取り除かれた
後、蛍光分析計９によって、蛍光強度が測定され、この
測定動作で得られた蛍光強度検知信号が膜濾過水流量目
標値演算装置５に供給されるとともに、濁質成分除去済
みの原水２が膜モジュール１０に供給され、原水２中の
有機物などの除去が行われる。After that, when the membrane filtration system 1a is put into operation and the raw water pump 8 is turned on, the pretreatment device for decontamination 7 takes in the raw water 2 to be treated, and the turbidity After the large turbidity component is removed from the components, the fluorescence intensity is measured by the fluorescence analyzer 9, and the fluorescence intensity detection signal obtained by this measurement operation is supplied to the membrane filtration water flow rate target value calculation device 5. In addition, the raw water 2 from which the turbidity components have been removed is supplied to the membrane module 10 to remove organic substances and the like from the raw water 2.

【００４８】また、この動作と並行し、膜濾過水流量目
標値演算装置５によって、膜濾過装置３から出力される
蛍光強度検知信号が取り込まれるとともに、膜濾過水流
量目標値／原水蛍光強度テーブル１４が参照されて、前
記蛍光強度検知信号で示される蛍光強度に対応する膜濾
過水流量目標値が求められ、この膜濾過水流量目標値を
示す膜濾過水流量目標値指示信号が流量一定制御装置６
に供給される。In parallel with this operation, the membranous filtered water flow rate target value calculation device 5 fetches the fluorescence intensity detection signal output from the membranous filtered device 3, and the membranous filtered water flow rate target value / raw water fluorescence intensity table. 14, the membrane filtration water flow rate target value corresponding to the fluorescence intensity indicated by the fluorescence intensity detection signal is obtained, and the membrane filtration water flow rate target value instruction signal indicating the membrane filtration water flow rate target value is controlled to be constant. Device 6
Is supplied to.

【００４９】また、この動作と並行し、流量調整弁バル
ブ１２、濾過水流量計１３によって、バルブの開度、濾
過水１１の流量が検知されて、バルブ開度検知信号、流
量検知信号が生成され、これらが流量一定制御装置６に
供給される。In parallel with this operation, the opening of the valve and the flow rate of the filtered water 11 are detected by the flow rate adjusting valve 12 and the filtered water flow meter 13 to generate a valve opening detection signal and a flow rate detection signal. Then, these are supplied to the constant flow rate control device 6.

【００５０】そして、流量一定制御装置６によって、膜
濾過水流量目標値演算装置５から出力される膜濾過水流
量目標値指示信号と、処理流量調整装置４から出力され
る流量検知信号とが比較され、これらの比較結果と、処
理流量調整装置４から出力されるバルブ開度検知信号と
に基づき、膜濾過水流量目標値と、濾過水流量とを一致
するのに必要なバルブ開度を示すバルブ開度指定信号が
生成され、これが流量調整弁１２に供給される。Then, the constant flow rate controller 6 compares the target membrane flow rate command value output signal from the target membrane flow rate calculator 5 with the flow rate detection signal output from the processing flow controller 4. Based on these comparison results and the valve opening detection signal output from the processing flow rate adjusting device 4, the valve opening required to match the membrane filtration water flow rate target value with the filtered water flow rate is shown. A valve opening designation signal is generated and supplied to the flow rate adjusting valve 12.

【００５１】これにより、流量調整弁１２のバルブ開度
が流量一定制御装置６から出力されるバルブ開度指定信
号の値に応じたバルブ開度にされて、膜濾過装置３から
送出される濾過水１１の通過流量が制御されながら、次
の処理に送水される。As a result, the valve opening degree of the flow rate adjusting valve 12 is adjusted to the valve opening degree according to the value of the valve opening degree designation signal output from the constant flow rate control device 6, and the filtration sent from the membrane filtration device 3 is performed. The water is sent to the next treatment while the flow rate of the water 11 is controlled.

【００５２】このように、第１実施形態によれば、原水
２の水質が季節によって変動しても、水質に応じて膜モ
ジュール１０に供給する原水の流量を最適化して、処理
流量を最適化でき、これによって膜間差圧上昇を抑えつ
つ、物理洗浄の回数、薬品洗浄の回数、濾過膜の交換回
数を低減してシステムの運転コストを低く抑えることが
できるとともに、膜処理水量を多くしてシステム稼働率
を高くすることができる。As described above, according to the first embodiment, even if the water quality of the raw water 2 varies depending on the season, the flow rate of the raw water supplied to the membrane module 10 is optimized according to the water quality, and the treatment flow rate is optimized. As a result, it is possible to reduce the number of times of physical cleaning, the number of chemical cleaning, and the number of times the filter membrane is replaced while suppressing the increase in the transmembrane pressure difference, and to keep the operating cost of the system low. System availability can be increased.

【００５３】また、この第１実施形態では、原水２を蛍
光分析計９に導いて、波長“３４５ｎｍ”の励起光を照
射し、原水２から発せられる波長“４２５ｎｍ”の蛍光
を選択して蛍光強度を測定するようにしてので、原水２
の有機物濃度を正確に測定することができる。Further, in the first embodiment, the raw water 2 is guided to the fluorescence analyzer 9 and is irradiated with the excitation light of the wavelength "345 nm", and the fluorescence of the wavelength "425 nm" emitted from the raw water 2 is selected for fluorescence. Since the strength is measured, the raw water 2
The organic matter concentration of can be accurately measured.

【００５４】〈変形例〉膜濾過装置３内に濁度計を配置
し、この濁度計によって、原水２の濁度を測定して得ら
れた濁度検知信号と、蛍光分析計９から出力される蛍光
強度検知信号とに基づき、膜濾過水流量目標演算装置５
に演算を行わせて、原水２の蛍光強度、濁度に応じた最
適な膜濾過水流量目標値を求めるようにしても良い。<Modification> A turbidity meter is arranged in the membrane filtration device 3, and the turbidity meter outputs the turbidity detection signal obtained by measuring the turbidity of the raw water 2 and the fluorescence analyzer 9. Membrane filtered water flow rate target calculation device 5 based on the detected fluorescence intensity signal
May be performed to calculate the optimum target value of the membrane filtration water flow rate according to the fluorescence intensity and turbidity of the raw water 2.

【００５５】これにより、原水２の蛍光強度に加えて、
原水２の濁度を加味した最適な膜濾過水流量目標値を求
めて、上述した第１実施形態より、さらに処理流量、濾
過膜に対する逆洗浄の開始時期を最適化して、膜間差圧
上昇を抑えつつ、物理洗浄の回数、薬品洗浄の回数、濾
過膜の交換回数を低減して、システムの運転コストを低
く抑えることができるとともに、膜処理水量を多くし
て、システム稼働率を高くすることができる。As a result, in addition to the fluorescence intensity of raw water 2,
The optimum membrane filtration water flow rate target value in which the turbidity of the raw water 2 is added is obtained, and the treatment flow rate and the start time of backwashing of the filtration membrane are further optimized to increase the transmembrane pressure difference from the above-described first embodiment. It is possible to reduce the number of times of physical cleaning, the number of times of chemical cleaning, and the number of times of exchanging filtration membranes while suppressing the operating cost of the system, while increasing the amount of membrane-treated water and increasing the system operating rate. be able to.

【００５６】《第２実施形態》第２実施形態を図５を参
照して説明する。なお、この図において、図１の各部と
対応する部分には同じ符号が付してある。<< Second Embodiment >> A second embodiment will be described with reference to FIG. In this figure, parts corresponding to those in FIG. 1 are designated by the same reference numerals.

【００５７】図５に示す膜濾過システム１ｂは、処理対
象となる原水２の蛍光強度を測定しながら、膜濾過処理
して、原水２中の有機物などを除去する膜濾過装置３
と、膜濾過装置３から送出される濾過水１１の蛍光強
度、流量を計測しながら、指定されたバルブ開度で、濾
過水１１を通過して、次の処理に送出する処理流量調整
装置２１と、処理流量調整装置２１から出力される蛍光
強度検知信号、膜濾過装置３から出力される蛍光強度検
知信号に基づき、膜濾過水流量目標値を演算する膜濾過
水流量目標値演算装置２２と、膜濾過水流量目標値演算
装置２２から出力される膜濾過水流量目標値指示信号、
処理流量調整装置２１から出力される流量検知信号など
に基づき、バルブ開度指定信号を生成して、処理流量調
整装置２１の流量を制御する流量一定制御装置６とを備
えている。The membrane filtration system 1b shown in FIG. 5 measures the fluorescence intensity of the raw water 2 to be treated while performing a membrane filtration treatment to remove organic substances and the like in the raw water 2.
And a processing flow rate adjusting device 21 which sends the filtered water 11 to the next process through the filtered water 11 at a specified valve opening while measuring the fluorescence intensity and the flow rate of the filtered water 11 sent from the membrane filtration device 3. And a membrane filtration water flow rate target value computing device 22 for computing a membrane filtration water flow rate target value based on the fluorescence intensity detection signal output from the processing flow rate adjustment device 21 and the fluorescence intensity detection signal output from the membrane filtration device 3. , A membrane filtration water flow rate target value instruction signal output from the membrane filtration water flow rate target value computing device 22,
Based on a flow rate detection signal output from the processing flow rate adjusting device 21 and the like, a constant flow rate control device 6 is provided for generating a valve opening designating signal and controlling the flow rate of the processing flow rate adjusting device 21.

【００５８】処理流量調整装置２１は、流量調整弁１２
と、濾過水流量計１３と、蛍光分析計２３とを備えてい
る。The processing flow rate adjusting device 21 includes a flow rate adjusting valve 12
And a filtered water flow meter 13 and a fluorescence analyzer 23.

【００５９】蛍光分析計２３は、濾過水流量計１３から
送水される濾過水１１に含まれている有機物濃度を測定
するのに最適な波長範囲“３４０〜３５０ｎｍ”内の特
定波長、例えば波長“３４５ｎｍ”の励起光を照射しな
がら、濾過水１１から発せられる蛍光のうち、濾過水１
１に含まれている有機物濃度を測定するのに最適な波長
範囲“４２０〜４３０ｎｍ”内の特定波長、例えば波長
“４２５ｎｍ”の蛍光を選択して、蛍光強度を測定し、
蛍光強度検知信号を生成し、これを膜濾過水流量目標値
演算装置２２に供給する。The fluorescence analyzer 23 has a specific wavelength within the optimum wavelength range “340 to 350 nm” for measuring the concentration of organic substances contained in the filtered water 11 sent from the filtered water flow meter 13, for example, a wavelength “wavelength”. Of the fluorescence emitted from the filtered water 11 while irradiating the excitation light of 345 nm ”, the filtered water 1
The fluorescence intensity is measured by selecting the fluorescence of a specific wavelength within the optimum wavelength range “420 to 430 nm”, for example, the wavelength of “425 nm”, which is optimum for measuring the concentration of the organic matter contained in 1.
A fluorescence intensity detection signal is generated and supplied to the membrane filtration water flow rate target value calculation device 22.

【００６０】膜濾過水流量目標値演算装置２２は、膜濾
過装置３から出力される蛍光強度検知信号と、処理流量
調整装置２１から出力される蛍光強度信号との差“Δ蛍
光強度”を求めるとともに、この差“Δ蛍光強度”と予
め設定されている基準値とを比較し、“Δ蛍光強度＜基
準値”にするのに必要な膜濾過水流量目標値を求め、膜
濾過水流量目標値指示信号を生成する演算部を備えてい
る。The membrane filtration water flow rate target value calculation device 22 obtains the difference "Δfluorescence intensity" between the fluorescence intensity detection signal output from the membrane filtration device 3 and the fluorescence intensity signal output from the processing flow rate adjustment device 21. At the same time, this difference “Δ fluorescence intensity” is compared with a preset reference value, and the membrane filtration water flow rate target value required to make “Δ fluorescence intensity <reference value” is obtained. A calculation unit that generates a value instruction signal is provided.

【００６１】次に、第２実施形態の動作を説明する。Next, the operation of the second embodiment will be described.

【００６２】まず、膜濾過システム１ｂが稼働状態にさ
れると、流量一定制御装置６によって、バルブ開度指定
信号が生成されて、流量調整弁１２に供給され、バルブ
の開度が初期設定開度にされるとともに、原水ポンプ８
がオン状態にされて、前の処理から送出されている原水
２の取り込み処理が開始される。First, when the membrane filtration system 1b is put into operation, the constant flow rate control device 6 generates a valve opening degree designation signal and supplies it to the flow rate adjusting valve 12 so that the opening degree of the valve is set to the initial setting. Raw water pump 8
Is turned on, and the process of taking in the raw water 2 sent from the previous process is started.

【００６３】これにより、除濁用前処理器７によって、
処理対象となる原水２が取り込まれて、濁質成分のう
ち、大きな濁質成分が取り除かれた後、膜濾過装置３の
蛍光分析計９によって、蛍光強度が測定され、この測定
動作で得られた蛍光強度検知信号が膜濾過水流量目標値
演算装置２２に供給されるとともに、濁質成分除去済み
の原水２が膜モジュール１０に供給され、原水２中の有
機物などの除去が行われ、有機物除去済みの原水（濾過
水１１）が処理流量調整装置２１に供給される。As a result, the pretreatment device 7 for turbidity removal
After the raw water 2 to be treated is taken in and the large turbidity components are removed from the turbidity components, the fluorescence intensity is measured by the fluorescence analyzer 9 of the membrane filtration device 3 and obtained by this measurement operation. The fluorescence intensity detection signal is supplied to the membrane filtration water flow rate target value calculation device 22, and the raw water 2 from which the turbidity components have been removed is supplied to the membrane module 10 to remove organic substances and the like in the raw water 2 to remove organic substances. The removed raw water (filtered water 11) is supplied to the processing flow rate adjusting device 21.

【００６４】また、この動作と並行し、処理流量調整装
置２１に設けられた濾過水流量計１３によって、膜モジ
ュール１０から送出される濾過水１１の流量が測定さ
れ、この測定動作で得られた流量検知信号が流量一定制
御装置６に供給されるとともに、処理流量調整装置２１
に設けられた蛍光分析計２３によって、膜モジュール１
１から送出される濾過水１１の蛍光強度が測定され、こ
の測定動作で得られた蛍光強度検知信号が膜濾過水流量
目標値演算装置２２に供給される。Further, in parallel with this operation, the flow rate of the filtered water 11 sent from the membrane module 10 was measured by the filtered water flow meter 13 provided in the treatment flow rate adjusting device 21 and obtained by this measuring operation. The flow rate detection signal is supplied to the constant flow rate controller 6 and the processing flow rate adjuster 21
With the fluorescence analyzer 23 provided in the membrane module 1
1, the fluorescence intensity of the filtered water 11 is measured, and the fluorescence intensity detection signal obtained by this measurement operation is supplied to the membrane filtered water flow rate target value calculation device 22.

【００６５】また、この動作と並行し、膜濾過水流量目
標値演算装置２２によって、膜濾過装置３から出力され
る蛍光強度検知信号、処理流量調整装置２１から出力さ
れる蛍光強度検知信号との差“Δ蛍光強度”が求めると
ともに、この差“Δ蛍光強度”と、予め設定されている
基準値とが比較され、この比較結果に基づき、“Δ蛍光
強度＜基準値”にするのに必要な膜濾過水流量目標値を
示す膜濾過水流量目標値指示信号が生成され、これが流
量一定制御装置６に供給される。In parallel with this operation, the fluorescence intensity detection signal output from the membrane filtration device 3 and the fluorescence intensity detection signal output from the processing flow rate adjustment device 21 are calculated by the membrane filtration water flow rate target value computing device 22. The difference “Δ fluorescence intensity” is calculated, and this difference “Δ fluorescence intensity” is compared with a preset reference value, and it is necessary to set “Δ fluorescence intensity <reference value” based on the comparison result. A membrane filtration water flow rate target value instruction signal indicating a desired membrane filtration water flow rate target value is generated and supplied to the constant flow rate control device 6.

【００６６】そして、流量一定制御装置６によって、膜
濾過水流量目標値演算装置２２から出力される膜濾過水
流量目標値指示信号と、処理流量調整装置２１から出力
される流量検知信号とが比較され、これらの比較結果
と、処理流量調整装置２１から出力されるバルブ開度検
知信号とに基づき、膜濾過水流量目標値と、濾過水流量
とを一致するのに必要なバルブ開度を示すバルブ開度指
定信号が生成され、これが流量調整弁１２に供給され
る。Then, the constant flow rate control device 6 compares the membrane filtration water flow rate target value instruction signal output from the membrane filtration water flow rate target value computing device 22 with the flow rate detection signal output from the processing flow rate adjusting device 21. Based on these comparison results and the valve opening detection signal output from the processing flow rate adjusting device 21, the valve opening required to match the membrane filtered water flow rate target value with the filtered water flow rate is shown. A valve opening designation signal is generated and supplied to the flow rate adjusting valve 12.

【００６７】この際、膜モジュール１０を薬品洗浄した
後、膜モジュール１０に対し、原水２を供給し続けて
も、原水２中の溶融性有機物をほとんど除去できず、原
水２の蛍光強度と、濾過水１１の蛍光強度とがほぼ同じ
値になることから、膜濾過システム１ｂが稼働状態にさ
れてから、所定期間、流量調整弁１２のバルブ開度が予
め設定されている開度にされて、膜濾過装置３から送出
される濾過水１１が次の処理に送水される。At this time, even if the raw water 2 is continuously supplied to the membrane module 10 after chemical cleaning of the membrane module 10, almost no fusible organic matter in the raw water 2 can be removed, and the fluorescence intensity of the raw water 2 Since the fluorescence intensity of the filtered water 11 has almost the same value, the valve opening degree of the flow rate adjusting valve 12 is set to a preset opening degree for a predetermined period after the membrane filtration system 1b is operated. The filtered water 11 sent from the membrane filtration device 3 is sent to the next process.

【００６８】この後、膜モジュール１０が定期的に物理
洗浄されながら、膜モジュール１０に対し、一定処理流
量で、一定水質の原水２が供給され続けられ、膜表面お
よび内部に付着した有機物や微生物などによって、原水
２中の溶融性有機物が吸着除去され、膜モジュール１０
から送出される濾過水１１に含まれている溶融性有機物
の濃度が低下し、処理流量調整装置２１の蛍光分析計２
３から出力されている蛍光強度検知信号の値が小さくな
り、“Δ蛍光強度≧基準値”になると、膜濾過水流量目
標値演算装置２２によって、膜濾過装置３から出力され
る蛍光強度検知信号、処理流量調整装置２１から出力さ
れる蛍光強度検知信号との差“Δ蛍光強度”を小さくす
るのに必要な膜濾過水流量目標値が求められ、この膜濾
過水流量目標値に基づき、流量一定制御装置６に供給さ
れている膜濾過水流量目標値指示信号の値が更新され
る。After that, while the membrane module 10 is regularly physically cleaned, the membrane module 10 is continuously supplied with the raw water 2 of a constant water quality at a constant treatment flow rate, and organic substances and microorganisms adhering to the membrane surface and the inside are kept. The meltable organic matter in the raw water 2 is adsorbed and removed by, for example, the membrane module 10
The concentration of the meltable organic matter contained in the filtered water 11 sent from the device decreases, and the fluorescence analyzer 2 of the processing flow rate adjusting device 21
When the value of the fluorescence intensity detection signal output from No. 3 becomes small and “Δfluorescence intensity ≧ reference value”, the fluorescence intensity detection signal output from the membrane filtration device 3 by the membrane filtration water flow rate target value calculation device 22. , The target value of the membrane filtered water flow rate required to reduce the difference “Δfluorescence intensity” from the fluorescence intensity detection signal output from the processing flow rate adjusting device 21 is obtained, and based on the target value of the membrane filtered water flow rate, The value of the membrane filtration water flow rate target value instruction signal supplied to the constant control device 6 is updated.

【００６９】これにより、流量一定制御装置６から出力
されるバルブ開度指定信号の値が小さくされ、処理流量
調整装置２１に設けられた流量調整弁１２のバルブ開度
が小さくされるとともに、膜濾過装置３から送出される
濾過水１１の流量が小さくされて、膜濾過装置３に設け
られている膜モジュール１０の膜間差圧が所定の値以下
に保持される。As a result, the value of the valve opening designating signal output from the constant flow rate control device 6 is reduced, the valve opening of the flow rate adjusting valve 12 provided in the processing flow rate adjusting device 21 is reduced, and the membrane The flow rate of the filtered water 11 delivered from the filtration device 3 is reduced, and the transmembrane pressure difference of the membrane module 10 provided in the membrane filtration device 3 is maintained below a predetermined value.

【００７０】このように、この第２実施形態では、処理
対象となる原水２の蛍光強度と、濾過水１１の蛍光強度
とを測定するとともに、これら原水２の蛍光強度と、濾
過水１１の蛍光強度とに基づいた“Δ蛍光強度”に応じ
て、処理水量を制御して、“Δ蛍光強度＜基準値”にす
るのに必要な膜濾過水流量目標値になるようにしなが
ら、原水２を膜濾過処理し、原水２中の有機物などを除
去して、次の処理に送水するようにした。As described above, in the second embodiment, the fluorescence intensity of the raw water 2 to be treated and the fluorescence intensity of the filtered water 11 are measured, and the fluorescence intensity of the raw water 2 and the fluorescence of the filtered water 11 are measured. The raw water 2 is controlled while controlling the amount of treated water according to the "Δ fluorescence intensity" based on the intensity so that the target value of the flow rate of the membrane filtered water is "Δ fluorescence intensity <reference value". Membrane filtration treatment was performed to remove organic substances and the like in raw water 2 and send the water to the next treatment.

【００７１】このため、原水２の水質が季節によって、
変動しても、膜モジュール１０の状態に応じて、膜モジ
ュール１０に供給する原水２の流量を最適化して、処理
流量を最適化することができる。Therefore, the water quality of the raw water 2 varies depending on the season.
Even if it fluctuates, the treatment flow rate can be optimized by optimizing the flow rate of the raw water 2 supplied to the membrane module 10 according to the state of the membrane module 10.

【００７２】また、この第２実施形態では、原水２を蛍
光分析計９に導かせて、波長“３４５ｎｍ”の励起光を
照射しながら、原水２から発せられる波長“４２５ｎ
ｍ”の蛍光を選択して、蛍光強度を測定するとともに、
濾過水１１を蛍光分析計２３に導かせて、波長“３４５
ｎｍ”の励起光を照射しながら、濾過水１１から発せら
れる波長“４２５ｎｍ”の蛍光を選択して、蛍光強度を
測定するようにした。Further, in the second embodiment, the raw water 2 is guided to the fluorescence analyzer 9 and irradiated with the excitation light of the wavelength "345 nm", and the wavelength "425n" emitted from the raw water 2 is emitted.
m "fluorescence is selected to measure the fluorescence intensity and
The filtered water 11 is guided to the fluorescence analyzer 23, and the wavelength of “345
While irradiating the excitation light of “nm”, the fluorescence of the wavelength “425 nm” emitted from the filtered water 11 was selected and the fluorescence intensity was measured.

【００７３】このため、原水２の有機物濃度のみなら
ず、濾過水１１の溶融性有機物濃度をも正確に測定する
ことができる。Therefore, not only the concentration of the organic matter in the raw water 2 but also the concentration of the soluble organic matter in the filtered water 11 can be accurately measured.

【００７４】〈変形例〉膜濾過装置３の蛍光分析計９か
ら出力される蛍光強度検知信号と、処理流量調整装置２
１の蛍光分析計２３から出力される蛍光強度検知信号を
逆洗浄制御装置（図示は省略する）に供給して、この逆
洗浄制御装置によって“Δ蛍光強度”を求め、この“Δ
蛍光強度”が予め設定されている洗浄開始設定値を超え
ているかどうかをチェックし、“Δ蛍光強度”が洗浄開
始設定値を超えているとき、膜モジュール１０の逆洗浄
を開始するようにしても良い。<Modification> The fluorescence intensity detection signal output from the fluorescence analyzer 9 of the membrane filtration device 3 and the processing flow rate adjusting device 2
The fluorescence intensity detection signal output from the fluorescence analyzer 23 of No. 1 is supplied to the backwash control device (not shown), and the “Δfluorescence intensity” is obtained by this backwash control device.
It is checked whether "fluorescence intensity" exceeds a preset cleaning start set value, and when "Δ fluorescence intensity" exceeds the wash start set value, back washing of the membrane module 10 is started. Is also good.

【００７５】これにより、原水２の有機物濃度に対応し
た蛍光強度と、濾過水１１の溶融性有機物濃度に対応し
た蛍光強度とを指標にして、膜モジュール１０に対する
逆洗浄の開始時期を最適化することができる。As a result, the start time of backwashing of the membrane module 10 is optimized by using the fluorescence intensity corresponding to the concentration of the organic matter in the raw water 2 and the fluorescence intensity corresponding to the concentration of the soluble organic matter in the filtered water 11 as indexes. be able to.

【００７６】《第３実施形態》第３実施形態を図６を参
照して説明する。なお、この図において、図１の各部と
対応する部分には、同じ符号が付してある。<< Third Embodiment >> A third embodiment will be described with reference to FIG. In this figure, parts corresponding to those in FIG. 1 are designated by the same reference numerals.

【００７７】図６に示す膜濾過システム１ｃは、処理対
象となる原水２の吸光度を測定しながら、膜濾過処理し
て、原水２中の有機物などを除去する膜濾過装置３１
と、膜濾過装置３１から送出される濾過水１１の流量を
計測しながら、指定されたバルブ開度で、濾過水１１を
通過して、次の処理に送出する処理流量調整装置４と、
膜濾過装置３１から出力される吸光度検知信号に基づ
き、膜濾過水流量目標値を演算する膜濾過水流量目標値
演算装置３２と、膜濾過水流量目標値演算装置３２から
出力される膜濾過水流量目標値指示信号、処理流量調整
装置４から出力される流量検知信号などに基づき、バル
ブ開度指定信号を生成して、処理流量調整装置４の流量
を制御する流量一定制御装置６とを備えている。The membrane filtration system 1c shown in FIG. 6 measures the absorbance of the raw water 2 to be treated while performing a membrane filtration treatment to remove organic substances and the like in the raw water 2.
And a processing flow rate adjusting device 4 which, while measuring the flow rate of the filtered water 11 sent from the membrane filtering device 31, passes through the filtered water 11 at a designated valve opening degree and sends it to the next processing,
Membrane filtered water flow rate target value calculation device 32 that calculates a membrane filtered water flow rate target value based on the absorbance detection signal output from the membrane filtration device 31, and membrane filtered water output from the membrane filtered water flow rate target value calculation device 32 A constant flow control device 6 for controlling the flow rate of the processing flow rate adjusting device 4 by generating a valve opening degree designating signal based on the flow rate target value instruction signal, the flow rate detection signal output from the processing flow rate adjusting device 4, and the like. ing.

【００７８】膜濾過装置３１は、前の処理から送水され
た原水２に含まれている濁質成分のうち、大きな濁質成
分を取り除く除濁用前処理器７と、除濁用前処理器７か
ら原水２を取り込む原水ポンプ８と、原水ポンプ８によ
って取り込まれた原水２に含まれている有機物濃度を測
定するのに最適な波長範囲“２６０〜２７０ｎｍ”内の
特定波長、例えば波長“２６０ｎｍ”の光に対する吸光
度を測定し、吸光度検知信号を生成する吸光度計３３
と、原水ポンプ８によって取り込まれた原水２を膜濾過
して、原水２に含まれている有機物などを除去する膜モ
ジュール１０とを備えている。The membrane filtration device 31 includes a turbidity pretreatment device 7 for removing large turbidity components from the turbidity components contained in the raw water 2 sent from the previous treatment, and a turbidity pretreatment device. A raw water pump 8 that takes in the raw water 2 from 7 and a specific wavelength within the optimum wavelength range “260 to 270 nm” for measuring the concentration of organic matter contained in the raw water 2 taken in by the raw water pump 8, for example, the wavelength “260 nm” Absorbance meter 33 for measuring the absorbance with respect to light and generating an absorbance detection signal
And a membrane module 10 for membrane-filtering the raw water 2 taken in by the raw water pump 8 to remove organic substances and the like contained in the raw water 2.

【００７９】処理流量調整装置４は、バルブの開度を検
知して、バルブ開度検知信号を生成し、これを流量一定
制御装置６に供給しながら、この流量一定制御装置６か
ら出力されるバルブ開度指定信号の値に応じてバルブを
開いて、膜濾過装置３１から送出される濾過水１１の通
過流量を調整する流量調整弁１２と、流量調整弁１２か
ら送水される濾過水１１の流量を測定し、流量検知信号
を生成し、これを流量一定制御装置６に供給しながら、
流量測定済みの濾過水１１を次の処理に送水する濾過水
流量計１３とを備えている。The processing flow rate adjusting device 4 detects the opening degree of the valve, generates a valve opening degree detection signal, and supplies it to the constant flow rate controlling device 6 while outputting it from the constant flow rate controlling device 6. According to the value of the valve opening designating signal, the valve is opened to adjust the flow rate of the filtered water 11 sent from the membrane filtration device 31, and the filtered water 11 sent from the flow rate adjusting valve 12. While measuring the flow rate, generating a flow rate detection signal, and supplying this to the constant flow rate control device 6,
A filtered water flow meter 13 for sending the filtered water 11 whose flow rate has been measured to the next process.

【００８０】膜濾過水流量目標値演算装置３１は、膜濾
過装置３１から出力される吸光度検知信号を取り込むと
ともに、設計データ、測定データなどによって得られる
膜濾過水流量目標値／原水吸光度テーブル３４（図９参
照）を参照しながら、前記吸光度検知信号で示される吸
光度に対応する膜濾過水流量目標値を求めて、膜濾過水
流量目標値指示信号を生成し、これを流量一定制御装置
６に供給する。The membrane filtration water flow rate target value calculation device 31 takes in the absorbance detection signal output from the membrane filtration device 31, and obtains the membrane filtration water flow rate target value / raw water absorbance table 34 ( Referring to FIG. 9), a membrane filtration water flow rate target value corresponding to the absorbance indicated by the absorbance detection signal is obtained, and a membrane filtration water flow rate target value instruction signal is generated. Supply.

【００８１】流量一定制御装置６は、膜濾過水流量目標
値演算装置３１から出力される膜濾過水流量目標値指示
信号で示される膜濾過水流量目標値と処理流量調整装置
４から出力される流量検知信号で示される濾過水流量と
を比較し、これらの比較結果と、処理流量調整装置４か
ら出力されるバルブ開度検知信号で示されるバルブ開度
とに基づき、膜濾過水流量目標値と、濾過水流量とを一
致するのに必要なバルブ開度を求めて、バルブ開度を示
すバルブ開度指定信号を処理流量調整装置４に供給す
る。The constant flow rate control device 6 outputs the membrane filtered water flow rate target value indicated by the membrane filtered water flow rate target value instruction signal output from the membrane filtered water flow rate target value calculation device 31 and the process flow rate adjusting device 4. The membrane filtered water flow rate target value is compared with the filtered water flow rate indicated by the flow rate detection signal, and based on these comparison results and the valve opening degree indicated by the valve opening degree detection signal output from the processing flow rate adjusting device 4. And a valve opening required to match the filtered water flow rate, and a valve opening designating signal indicating the valve opening is supplied to the processing flow rate adjusting device 4.

【００８２】次に、第３実施形態の動作を説明する。Next, the operation of the third embodiment will be described.

【００８３】まず、膜濾過システム１ｃを稼働する前
に、次に述べる手順で、膜濾過水流量目標値／原水吸光
度テーブル３４が作成される。First, before operating the membrane filtration system 1c, the membrane filtration water flow rate target value / raw water absorbance table 34 is created by the following procedure.

【００８４】一般的に、膜モジュール１０を定期的に物
理洗浄しながら、膜モジュール１０に対し、一定処理流
量で、一定水質の原水２を供給し、膜濾過し続けると、
図７の膜濾過時間／膜間差圧グラフに示すように、膜濾
過の経過時間に応じて、膜間差圧が上昇し、予め設定さ
れている薬品洗浄開始膜間差圧値を越える毎に、薬品洗
浄を行わなければならない。Generally, while physically cleaning the membrane module 10 periodically, the raw water 2 having a constant water quality is supplied to the membrane module 10 at a constant treatment flow rate and the membrane filtration is continued.
As shown in the membrane filtration time / membrane pressure difference graph of FIG. 7, the membrane pressure difference increases according to the elapsed time of membrane filtration, and every time the preset value of the chemical cleaning start membrane pressure difference value is exceeded. First, chemical cleaning must be performed.

【００８５】このとき、原水２の流量を“６０Ｌ／ｈｒ
／ｍ２”にしたときに比べて、“４０Ｌ／ｈｒ／ｍ２”
にした方が膜モジュール１０内の濾過膜に負担をかける
ことなく、膜濾過時間を長くして、薬品洗浄回数を低減
することができる。At this time, the flow rate of the raw water 2 is set to "60 L / hr.
/ "Than when you," m 2 40L / hr / m 2 "
It is possible to extend the membrane filtration time and reduce the number of times of chemical cleaning without imposing a burden on the filtration membrane in the membrane module 10.

【００８６】また、膜モジュール１０に供給する原水２
に含まれる有機物が多くなり、波長“２６０ｎｍ”の光
に対する原水２の吸光度が大きくなると、図８の膜間差
圧上昇率／膜濾過水流量グラフに示すように、最大許容
差圧上昇率以下にするのに必要な膜濾過水量が小さくな
る。Further, the raw water 2 supplied to the membrane module 10
When the amount of organic matter contained in the water increases and the absorbance of the raw water 2 with respect to the light of the wavelength “260 nm” increases, as shown in the graph of transmembrane pressure difference / membrane filtered water flow rate graph shown in FIG. The amount of membrane-filtered water required to achieve this is reduced.

【００８７】そして、図８に示す差圧上昇率と、図７に
示す膜間差圧の傾き（差圧上昇率）とが対応しているこ
とから、これら図７に示す膜濾過時間／膜間差圧グラフ
と、図８の膜間差圧上昇率／膜濾過水流量グラフとに基
づき、図９に示すように、膜モジュール内に設けられた
濾過膜の最大許容差圧上昇率を越えないようにしなが
ら、薬品洗浄回数を少なくするために必要な膜濾過水流
量目標値／原水吸光度テーブル３４が作成されて、これ
が膜濾過流量目標値演算装置３２に格納される。Since the differential pressure increase rate shown in FIG. 8 corresponds to the transmembrane pressure difference slope (differential pressure increase rate) shown in FIG. 7, the membrane filtration time / membrane shown in FIG. Based on the differential pressure graph and the transmembrane pressure increase rate / membrane filtered water flow rate graph of FIG. 8, as shown in FIG. 9, the maximum allowable differential pressure increase rate of the filtration membrane provided in the membrane module is exceeded. The membrane filtration water flow rate target value / raw water absorbance table 34 required to reduce the number of times of chemical cleaning is created, and stored in the membrane filtration flow rate target value calculation device 32.

【００８８】この後、膜濾過システム１ｃが稼働状態に
されて、原水ポンプ８がオン状態にされると、除濁用前
処理器７によって、処理対象となる原水２が取り込まれ
て、濁質成分のうち、大きな濁質成分が取り除かれた
後、吸光度計３３によって、波長“２６０ｎｍ”の光に
対する吸光度が測定され、この測定動作で得られた吸光
度検知信号が膜濾過水流量目標値演算装置３２に供給さ
れるとともに、濁質成分除去済みの原水２が膜モジュー
ル１０に供給され、原水２中の有機物などの除去が行わ
れる。After that, when the membrane filtration system 1c is put into operation and the raw water pump 8 is turned on, the pretreatment device for decontamination 7 takes in the raw water 2 to be treated, and the turbidity After removing the large turbid component from the components, the absorbance for the light of wavelength "260 nm" is measured by the absorptiometer 33, and the absorbance detection signal obtained by this measurement operation is the membrane filtration water flow rate target value computing device. While being supplied to 32, the raw water 2 from which turbidity components have been removed is supplied to the membrane module 10 to remove organic substances and the like in the raw water 2.

【００８９】また、この動作と並行し、膜濾過水流量目
標値演算装置３２によって、膜濾過装置３１から出力さ
れる吸光度検知信号が取り込まれるとともに、膜濾過水
流量目標値／原水吸光度テーブル３４が参照されて、前
記吸光度検知信号で示される吸光度に対応する膜濾過水
流量目標値が求められ、この膜濾過水流量目標値を示す
膜濾過水流量目標値指示信号が流量一定制御装置６に供
給される。In parallel with this operation, the membrane filtration water flow rate target value calculation device 32 fetches the absorbance detection signal output from the membrane filtration device 31, and the membrane filtration water flow rate target value / raw water absorbance table 34 is displayed. The membrane filtration water flow rate target value corresponding to the absorbance indicated by the absorbance detection signal is obtained by reference, and the membrane filtration water flow rate target value instruction signal indicating the membrane filtration water flow rate target value is supplied to the constant flow rate control device 6. To be done.

【００９０】また、この動作と並行し、流量調整弁１
２、濾過水流量計１３によって、バルブの開度、濾過水
１１の流量が検知されて、バルブ開度検知信号、流量検
知信号が生成され、これらが流量一定制御装置６に供給
される。In parallel with this operation, the flow rate adjusting valve 1
2. The filtered water flow meter 13 detects the valve opening and the flow rate of the filtered water 11 to generate a valve opening detection signal and a flow rate detection signal, which are supplied to the constant flow rate control device 6.

【００９１】そして、流量一定制御装置６によって、膜
濾過水流量目標値演算装置３２から出力される膜濾過水
流量目標値指示信号と、処理流量調整装置４から出力さ
れる流量検知信号とが比較され、これらの比較結果と、
処理流量調整装置４から出力されるバルブ開度検知信号
とに基づき、膜濾過水流量目標値と、濾過水流量とを一
致するのに必要なバルブ開度を示すバルブ開度指定信号
が生成され、これが流量調整弁１２に供給される。Then, the constant flow rate control device 6 compares the membrane filtered water flow rate target value instruction signal output from the membrane filtered water flow rate target value calculation device 32 with the flow rate detection signal output from the processing flow rate adjusting device 4. And these comparison results,
Based on the valve opening degree detection signal output from the processing flow rate adjusting device 4, a valve opening degree designation signal indicating a valve opening degree necessary to match the membrane filtration water flow rate target value with the filtered water flow rate is generated. , Which is supplied to the flow rate adjusting valve 12.

【００９２】これにより、流量調整弁１２のバルブ開度
が流量一定制御装置６から出力されるバルブ開度指定信
号の値に応じたバルブ開度にされて、膜濾過装置３１か
ら送出される濾過水１１の通過流量が制御される。As a result, the valve opening degree of the flow rate adjusting valve 12 is adjusted to the valve opening degree according to the value of the valve opening degree designation signal output from the constant flow rate control device 6, and the filtration sent from the membrane filtration device 31. The flow rate of the water 11 is controlled.

【００９３】このように、この第３実施形態では、処理
対象となる原水２の吸光度を測定するとともに、吸光度
に応じて処理水量が膜濾過水流量目標値になるように制
御して原水２を膜濾過処理するようにした。As described above, in the third embodiment, the absorbance of the raw water 2 to be treated is measured, and the raw water 2 is controlled by controlling the treated water amount so as to reach the membrane filtration water flow rate target value according to the absorbance. Membrane filtration was performed.

【００９４】このため、原水２の水質が季節によって変
動しても、水質に応じて膜モジュール１０に供給する原
水の流量を最適化し、処理流量を最適化することがで
き、これによって膜間差圧上昇を抑えつつ、物理洗浄の
回数、薬品洗浄の回数、濾過膜の交換回数を低減して、
システムの運転コストを低く抑えることができるととも
に、膜処理水量を多くして、システム稼働率を高くする
ことができる。Therefore, even if the water quality of the raw water 2 changes depending on the season, the flow rate of the raw water supplied to the membrane module 10 can be optimized according to the water quality, and the treatment flow rate can be optimized. While suppressing the pressure rise, the number of physical cleaning, chemical cleaning and filter membrane replacement can be reduced.
The operating cost of the system can be kept low, and the amount of membrane-treated water can be increased to increase the system operating rate.

【００９５】また、この第３実施形態では、原水２に吸
光度計３３に導かせて、波長“２６０ｎｍ”の光に対す
る吸光度を測定するようにした。このため、原水２の有
機物濃度を正確に測定することができ、これによって処
理流量、濾過膜に対する逆洗浄の開始時期を最適化する
ことができる。Further, in the third embodiment, the raw water 2 is introduced into the absorptiometer 33, and the absorptance to the light of wavelength "260 nm" is measured. Therefore, the concentration of organic matter in the raw water 2 can be accurately measured, and thereby the treatment flow rate and the start time of backwashing of the filtration membrane can be optimized.

【００９６】〈変形例〉膜濾過装置３１内に濁度計を配
置し、この濁度計によって、原水２の濁度を測定して得
られた濁度検知信号と、吸光度計３３から出力される吸
光度検知信号とに基づき、膜濾過水流量目標演算装置３
２に演算を行わせて、原水２の吸光度、濁度に応じた最
適な膜濾過水流量目標値を求めるようにしても良い。<Modification> A turbidity meter is arranged in the membrane filtration device 31, and the turbidity meter outputs the turbidity detection signal obtained by measuring the turbidity of the raw water 2 and the absorptiometer 33. Membrane filtered water flow rate target calculation device 3 based on the absorbance detection signal
2 may be calculated to obtain the optimum membrane-filtered water flow rate target value according to the absorbance and turbidity of the raw water 2.

【００９７】これにより、原水２の吸光度に加えて、原
水２の濁度を加味した、最適な膜濾過水流量目標値を求
めて、上述した第３実施形態より、さらに処理流量、濾
過膜に対する逆洗浄の開始時期を最適化して、膜間差圧
上昇を抑えつつ、物理洗浄の回数、薬品洗浄の回数、濾
過膜の交換回数を低減して、システムの運転コストを低
く抑えることができるとともに、膜処理水量を多くし
て、システム稼働率を高くすることができる。As a result, the optimum membrane-filtered water flow rate target value, in which the turbidity of the raw water 2 is taken into consideration in addition to the absorbance of the raw water 2, is obtained, and the treatment flow rate and the filtration membrane are further changed from the above-described third embodiment. By optimizing the start time of backwashing and suppressing the rise of transmembrane pressure difference, the number of physical washes, the number of chemical washes, and the number of exchanges of filtration membranes can be reduced, and the operating cost of the system can be kept low. It is possible to increase the system treatment rate by increasing the amount of membrane-treated water.

【００９８】また、処理流量調整装置４にも、波長“２
６０ｎｍ”の光に対する吸光度を測定する吸光度計を配
置し、この吸光度計から出力される吸光度検知信号と、
膜濾過装置３１の吸光度計３３から出力される吸光度検
知信号とに基づき、膜濾過水流量目標値演算装置３２に
膜濾過水流量目標値／原水吸光度テーブル３４を用いた
演算、あるいは“Δ吸光度”などを用いた演算などを行
わせて、原水２の吸光度、濾過水１１の吸光度に応じた
最適な膜濾過水流量目標値を求めるようにしても良い。Further, the processing flow rate adjusting device 4 also has a wavelength "2".
An absorptiometer for measuring the absorptivity for light of 60 nm "is arranged, and an absorbance detection signal output from the absorptiometer,
Based on the absorbance detection signal output from the absorptiometer 33 of the membrane filtration device 31, the membrane filtration water flow rate target value computing device 32 uses the membrane filtration water flow rate target value / raw water absorbance table 34 to calculate, or "Δabsorbance" It is also possible to calculate the optimum target value of the flow rate of the membrane-filtered water according to the absorbance of the raw water 2 and the absorbance of the filtered water 11 by performing calculations using the above.

【００９９】これにより、原水２の吸光度に加えて、濾
過水１１の吸光度を加味した、最適な膜濾過水流量目標
値を求めて、原水２の水質が季節によって、変動して
も、膜モジュール１０の状態に応じて、膜モジュール１
０に供給する原水２の流量を最適化して、処理流量を最
適化し、これによって膜間差圧上昇を抑えつつ、物理洗
浄の回数、薬品洗浄の回数、濾過膜の交換回数を低減し
て、システムの運転コストを低く抑えることができると
ともに、膜処理水量を多くして、システム稼働率を高く
することができる。As a result, the optimum membrane-filtered water flow rate target value, which takes into account the absorbance of the filtered water 11 in addition to the absorbance of the raw water 2, is calculated, and even if the water quality of the raw water 2 changes depending on the season, Membrane module 1 according to 10 states
By optimizing the flow rate of the raw water 2 supplied to 0, the treatment flow rate is optimized, thereby suppressing the increase in transmembrane pressure difference, and reducing the number of times of physical cleaning, the number of chemical cleaning, and the number of times of replacement of the filtration membrane, The operating cost of the system can be kept low, and the amount of membrane-treated water can be increased to increase the system operating rate.

【０１００】さらに、処理流量調整装置４にも、波長
“２６０ｎｍ”の光に対する吸光度を測定する吸光度計
を配置し、この吸光度計から出力される吸光度検知信号
と、膜濾過装置３１の吸光度計３３から出力される吸光
度検知信号とを逆洗浄制御装置（図示は省略する）に供
給して、この逆洗浄制御装置に“Δ吸光度”を求めると
ともに、この“Δ吸光度”が予め設定されている洗浄開
始設定値を超えているかどうかをチェックし、“Δ吸光
度”が洗浄開始設定値を超えているとき、膜モジュール
１０の逆洗浄を開始するようにしても良い。Further, the processing flow rate adjusting device 4 is also provided with an absorptiometer for measuring the absorptivity to the light of wavelength "260 nm", and the absorptiometry signal output from this absorptiometer and the absorptiometer 33 of the membrane filtration device 31 are arranged. The absorbance detection signal output from the backwash controller is supplied to a backwash controller (not shown) to obtain "Δabsorbance" in the backwash controller, and this "∆absorbance" is preset. It is also possible to check whether or not the start set value is exceeded, and when “Δabsorbance” exceeds the wash start set value, start backwashing of the membrane module 10.

【０１０１】これにより、原水２の有機物濃度に対応し
た蛍光強度と、濾過水１１の溶融性有機物濃度に対応し
た蛍光強度とを指標にして、膜モジュール１０に対する
逆洗浄の開始時期を最適化することができ、これによっ
て膜間差圧上昇を抑えつつ、物理洗浄の回数、薬品洗浄
の回数、濾過膜の交換回数を低減して、システムの運転
コストを低く抑えることができるとともに、膜処理水量
を多くして、システム稼働率を高くすることができる。Thus, the start time of backwashing of the membrane module 10 is optimized by using the fluorescence intensity corresponding to the concentration of the organic matter in the raw water 2 and the fluorescence intensity corresponding to the concentration of the soluble organic matter in the filtered water 11 as indexes. As a result, it is possible to reduce the number of times of physical cleaning, the number of chemical cleaning, and the number of times the filtration membrane is replaced while suppressing the increase in the transmembrane pressure difference, and to keep the operating cost of the system low, and to reduce the amount of membrane-treated water. Can be increased to increase the system operating rate.

【０１０２】《第４実施形態》次に第４実施形態を説明
する。なお、基本的なシステム構成は図５と同一である
ため、図５を用いてその特徴部分のみを説明する。<< Fourth Embodiment >> Next, a fourth embodiment will be described. Since the basic system configuration is the same as that in FIG. 5, only the characteristic part will be described with reference to FIG.

【０１０３】第４実施形態の特徴は、吸光度計４３にあ
る。この吸光度計４３は、原水ポンプ８によって取り込
まれた原水２に予め設定されている波長、例えば原水２
に含まれる、フミン酸（植物などが微生物により分解さ
れて生成された種々雑多な有機化合物によって構成され
る高分子有機化合物であり、樹木など、植物のセルロー
スやリグニン酸が酸化される過程で生じ、河川水着色の
原因物質となる黄褐色の色調を示す酸）の濃度を測定す
るのに最適な波長範囲“３８０〜４００ｎｍ”内の特定
波長、例えば波長“３８０ｎｍ”の光に対する吸光度を
測定し、吸光度検知信号を生成するものである。The feature of the fourth embodiment resides in the absorbance meter 43. The absorptiometer 43 has a wavelength preset in the raw water 2 taken in by the raw water pump 8, for example, the raw water 2
Humic acid (a high molecular weight organic compound composed of various organic compounds produced by the decomposition of microorganisms such as plants) contained in , The absorbance of light having a specific wavelength within the wavelength range of "380 to 400 nm", for example, the wavelength of "380 nm", which is optimal for measuring the concentration of the yellowish brown color that is the causative agent of river water coloring. , To generate an absorbance detection signal.

【０１０４】このように、この第４実施形態では、処理
対象となる原水２の吸光度を測定するとともに、吸光度
に応じて、処理水量を制御して、膜濾過水流量目標値に
なるようにしながら、原水２を膜濾過処理し、原水２中
の有機物などを除去して、次の処理に送水するようにし
ているので、原水２の水質が季節によって、変動して
も、水質に応じて、膜モジュール１０に供給する原水の
流量を最適化して、処理流量を最適化し、これによって
膜間差圧上昇を抑えつつ、物理洗浄の回数、薬品洗浄の
回数、濾過膜の交換回数を低減して、システムの運転コ
ストを低く抑えることができるとともに、膜処理水量を
多くして、システム稼働率を高くすることができる。As described above, in the fourth embodiment, the absorbance of the raw water 2 to be treated is measured, and the amount of treated water is controlled according to the absorbance to achieve the target value of the membrane filtered water flow rate. Since the raw water 2 is subjected to membrane filtration treatment to remove organic substances and the like from the raw water 2 and then sent to the next treatment, even if the water quality of the raw water 2 changes depending on the season, By optimizing the flow rate of the raw water supplied to the membrane module 10 and optimizing the treatment flow rate, the number of times of physical cleaning, the number of times of chemical cleaning, and the number of times of replacement of the filtration membrane are reduced while suppressing an increase in transmembrane pressure difference. It is possible to keep the operating cost of the system low, increase the amount of membrane-treated water, and increase the system operating rate.

【０１０５】また、この第４実施形態では、原水２に吸
光度計４３に導かせて、波長“３８０ｎｍ”の光に対す
る吸光度を測定するようにしているので、原水２の有機
物濃度のうち、フミン酸の濃度などを正確に測定するこ
とができ、これによって処理流量、濾過膜に対する逆洗
浄の開始時期を最適化して、膜間差圧上昇を抑えつつ、
物理洗浄の回数、薬品洗浄の回数、濾過膜の交換回数を
低減して、システムの運転コストを低く抑えることがで
きるとともに、膜処理水量を多くして、システム稼働率
を高くすることができる。In the fourth embodiment, the raw water 2 is introduced into the absorptiometer 43 to measure the absorbance for light having a wavelength of "380 nm". It is possible to accurately measure the concentration of water and the like, which optimizes the treatment flow rate and the start time of backwashing for the filtration membrane, while suppressing the increase in transmembrane pressure difference.
It is possible to reduce the operating cost of the system by reducing the number of times of physical cleaning, the number of times of chemical cleaning, and the number of times the filtration membrane is replaced, and increase the amount of membrane-treated water to increase the system operating rate.

【０１０６】〈変形例〉処理流量調整装置４にも、波長
“３８０ｎｍ”の光に対する吸光度を測定する吸光度計
を配置し、この吸光度計から出力される吸光度検知信号
と、膜濾過装置４１の吸光度計３３から出力される吸光
度検知信号とに基づき、膜濾過水流量目標値演算装置３
２に膜濾過水流量目標値／原水吸光度テーブル３４を用
いた演算、あるいは“Δ吸光度”などを用いた演算など
を行わせて、原水２の吸光度、濾過水１１の吸光度に応
じた最適な膜濾過水流量目標値を求めるようにしても良
い。<Modification> The processing flow rate adjusting device 4 is also provided with an absorptiometer for measuring the absorptance with respect to the light of the wavelength “380 nm”, and the absorbance detection signal output from the absorptiometer and the absorbance of the membrane filtration device 41 are arranged. Membrane filtered water flow rate target value calculation device 3 based on the absorbance detection signal output from the total 33
2 is calculated by using the target value of membrane filtered water flow rate / raw water absorbance table 34, or the calculation using “Δabsorbance”, etc., to obtain the optimum membrane according to the absorbance of raw water 2 and the absorbance of filtered water 11. The filtered water flow rate target value may be obtained.

【０１０７】また、処理流量調整装置４にも、波長“３
８０ｎｍ”の光に対する吸光度を測定する吸光度計を配
置し、この吸光度計から出力される吸光度検知信号と、
膜濾過装置３１の吸光度計３３から出力される吸光度検
知信号とを逆洗浄制御装置（図示は省略する）に供給し
て、この逆洗浄制御装置に“Δ吸光度”を求めるととも
に、この“Δ吸光度”が予め設定されている洗浄開始設
定値を超えているかどうかをチェックし、“Δ吸光度”
が洗浄開始設定値を超えているとき、膜モジュール１０
の逆洗浄を開始するようにしても良い。Further, the processing flow rate adjusting device 4 also has a wavelength of "3".
An absorptiometer for measuring the absorptivity for light of 80 nm "is arranged, and an absorbance detection signal output from the absorptiometer,
The absorbance detection signal output from the absorptiometer 33 of the membrane filtration device 31 is supplied to a backwash control device (not shown) to obtain "Δabsorbance" in the backwash control device, and the "Δabsorbance" is calculated. Check whether "exceeds the preset washing start set value,
Is above the cleaning start set value, the membrane module 10
It is also possible to start the reverse cleaning of.

【０１０８】《第５実施形態》第５実施形態を図１０を
参照して説明する。なお、この図において、図１の各部
と対応する部分には、同じ符号が付してある。<< Fifth Embodiment >> A fifth embodiment will be described with reference to FIG. In this figure, parts corresponding to those in FIG. 1 are designated by the same reference numerals.

【０１０９】図１０に示す膜濾過システム１ｄは、膜濾
過装置５１と、処理流量調整装置５２と、洗浄水供給装
置５４と、洗浄排水濁度検知装置５６と、膜濾過制御装
置５７とを備えている。The membrane filtration system 1d shown in FIG. 10 comprises a membrane filtration device 51, a treatment flow rate control device 52, a wash water supply device 54, a wash drainage turbidity detection device 56, and a membrane filtration control device 57. ing.

【０１１０】膜濾過装置５１は、前の処理から送水され
た原水２に含まれている濁質成分のうち、大きな濁質成
分を取り除く除濁用前処理器７と、膜濾過制御装置５７
からポンプオン信号が出力されているとき、オン状態に
なって、除濁用前処理器７から原水２を取り込む原水ポ
ンプ８と、原水ポンプ８によって取り込まれた原水２を
膜濾過して、原水２に含まれている有機物などを除去す
る膜モジュール１０とを備えている。The membrane filtration device 51 includes a turbidity pretreatment device 7 for removing large turbidity components from the turbidity components contained in the raw water 2 sent from the previous treatment, and a membrane filtration control device 57.
When a pump-on signal is output from the raw water pump 2, the raw water pump 8 is turned on to take in the raw water 2 from the pretreatment device for clarification 7, and the raw water 2 taken in by the raw water pump 8 is subjected to membrane filtration to obtain the raw water 2 And a membrane module 10 for removing organic substances and the like contained in.

【０１１１】処理流量調整装置５２は、バルブの開度を
検知して、バルブ開度検知信号を生成し、これを膜濾過
制御装置５７に供給しながら、この膜濾過制御装置５７
から出力されるバルブ開度指定信号の値に応じてバルブ
を開いて、膜濾過装置５１から送出される濾過水１１の
通過流量を調整する流量調整弁１２と、流量調整弁１２
から送水される濾過水１１の流量を測定して、流量検知
信号を生成し、これを膜濾過制御装置５７に供給する濾
過水流量計１３と、濾過水流量計１３から送水される濾
過水１１を一時貯留しながら、次の処理に送水する濾過
水タンク５８とを備えている。The processing flow rate adjusting device 52 detects the opening of the valve, generates a valve opening detection signal, and supplies this to the membrane filtration control device 57, while the membrane filtration control device 57 is being supplied.
The flow rate adjusting valve 12 that adjusts the passage flow rate of the filtered water 11 sent from the membrane filtration device 51 by opening the valve according to the value of the valve opening designation signal output from the flow rate adjusting valve 12.
The flow rate of the filtered water 11 sent from the filtered water flow meter 13 that generates a flow rate detection signal and supplies it to the membrane filtration control device 57, and the filtered water flow rate 11 sent from the filtered water flow meter 13 And a filtered water tank 58 for sending water to the next treatment.

【０１１２】洗浄水供給装置５４は、膜濾過制御装置５
７からポンプオン信号が出力されているとき、オン状態
になって、濾過水タンク５８から濾過水１１を取り込
み、洗浄水５３として送出する逆洗ポンプ５９と、バル
ブの開閉を検知して、バルブ開閉検知信号を生成し、こ
れを膜濾過制御装置５７に供給しながら、この膜濾過制
御装置５７からバルブ開指示信号が出力されていると
き、バルブを開いて、逆洗ポンプ５９から送出される洗
浄水５３を通過して、膜濾過装置５１の膜モジュール１
０に供給する逆洗弁６０とを備えている。The wash water supply unit 54 is the membrane filtration control unit 5.
When the pump-on signal is output from 7, the backwash pump 59 is turned on and takes in the filtered water 11 from the filtered water tank 58 and sends it as the washing water 53, and the opening / closing of the valve is detected to open / close the valve. While the detection signal is generated and supplied to the membrane filtration control device 57, when the valve opening instruction signal is output from the membrane filtration control device 57, the valve is opened and the washing is sent from the backwash pump 59. The membrane module 1 of the membrane filtration device 51 is passed through the water 53.
And a backwash valve 60 for supplying 0.

【０１１３】洗浄排水濁度検知装置５６は、バルブの開
閉を検知して、バルブ開閉検知信号を生成し、これを膜
濾過制御装置５７に供給しながら、この膜濾過制御装置
５７からバルブ開指示信号が出力されているとき、バル
ブを開いて、膜濾過装置５１の膜モジュール１０から送
出される洗浄排水５５を通過し、排水するドレン弁６２
と、ドレン弁６２から排水される洗浄排水５５の濁度を
測定して、濁度検知信号を生成し、これを膜濾過制御装
置５７に供給する濁度計６１とを備えている。The cleaning drainage turbidity detection device 56 detects opening / closing of the valve, generates a valve opening / closing detection signal, and supplies this signal to the membrane filtration control device 57, while instructing the valve opening from this membrane filtration control device 57. When the signal is output, the drain valve 62 that opens the valve and passes through and drains the cleaning drainage 55 sent from the membrane module 10 of the membrane filtration device 51.
And a turbidity meter 61 that measures the turbidity of the cleaning drainage 55 drained from the drain valve 62 to generate a turbidity detection signal and supplies the turbidity detection signal to the membrane filtration control device 57.

【０１１４】膜濾過制御装置５７は、稼働指示が入力さ
れたとき、膜濾過処理指示の生成を開始し、予め設定さ
れている期間が経過する毎に、膜濾過処理指示の生成を
停止して、物理洗浄処理指示の生成を開始し、逆洗洗浄
完了指示が入力されたとき、物理洗浄処理指示の生成を
停止して、膜濾過処理指示の生成を開始するシーケンサ
部と、図１１に示す洗浄時間／物理洗浄排水濁度テーブ
ル６２を持ち、シーケンサ部の出力、膜濾過装置５１の
出力、処理流量調整装置５２の出力、洗浄水供給装置５
４の出力、洗浄排水濁度検知装置５６の出力などに基づ
き、膜濾過装置５１、処理流量調整装置５２、洗浄水供
給装置５４、洗浄排水濁度検知装置５６を制御して、原
水２の膜濾過処理、膜モジュール１０の逆洗処理を交互
に行わせる制御部とを備えている。When the operation instruction is input, the membrane filtration control device 57 starts the generation of the membrane filtration processing instruction, and stops the generation of the membrane filtration processing instruction every time a preset period elapses. 11, a sequencer unit that starts the generation of the physical cleaning process instruction and, when the backwash cleaning completion command is input, stops the generation of the physical cleaning process instruction and starts the generation of the membrane filtration process instruction. Having a cleaning time / physical cleaning drainage turbidity table 62, output of the sequencer unit, output of the membrane filtration device 51, output of the processing flow rate adjusting device 52, cleaning water supply device 5
4, the membrane filtration device 51, the treatment flow rate adjusting device 52, the wash water supply device 54, and the wash drainage turbidity detector 56 are controlled based on the output of the washing water turbidity detector 56, and the membrane of the raw water 2 A control unit for alternately performing the filtration process and the backwashing process of the membrane module 10 is provided.

【０１１５】次に、第５実施形態の動作を説明する。Next, the operation of the fifth embodiment will be described.

【０１１６】まず、膜濾過システム１ｅの電源が投入さ
れて、稼働指示が入力されると、膜濾過制御装置５７に
よって、膜濾過処理が開始されて、処理流量調整装置５
２の濾過水流量計１３から出力される流量検知信号が取
り込まれるとともに、この流量検知信号で示される実流
量値と、予め設定されている設定処理流量値とが比較さ
れる。First, when the power of the membrane filtration system 1e is turned on and the operation instruction is input, the membrane filtration control device 57 starts the membrane filtration process and the process flow rate adjusting device 5 is started.
The flow rate detection signal output from the second filtered water flow meter 13 is taken in, and the actual flow rate value indicated by this flow rate detection signal is compared with the preset processing flow rate value.

【０１１７】次いで、この比較結果と、処理流量調整装
置５２の流量調整弁１２から出力されるバルブ開度検知
信号の値（バルブ開度）とに基づき、膜濾過制御装置５
７によって、“設定処理流量値≧実流量値”にするのに
必要なバルブ開度指定信号が生成され、これが処理流量
調整装置５２の流量調整弁１２に供給されて、流量調整
弁１２のバルブ開度が調整されるとともに、ポンプオン
信号が生成されて、これが膜濾過装置５１の原水ポンプ
８に供給される。Next, based on this comparison result and the value of the valve opening detection signal (valve opening) output from the flow rate adjusting valve 12 of the processing flow rate adjusting device 52, the membrane filtration control device 5
7, a valve opening degree designating signal necessary for satisfying “set processing flow rate value ≧ actual flow rate value” is generated, and this is supplied to the flow rate adjusting valve 12 of the process flow rate adjusting device 52, and the valve of the flow rate adjusting valve 12 is supplied. The opening degree is adjusted and a pump-on signal is generated and supplied to the raw water pump 8 of the membrane filtration device 51.

【０１１８】これにより、原水ポンプ８がオン状態にさ
れ、除濁用前処理器７によって、処理対象となる原水２
が取り込まれ、濁質成分のうち、大きな濁質成分が取り
除かれた後、濁質成分除去済みの原水２が膜モジュール
１０に供給され、原水２中の有機物などの除去が行われ
た後、この膜濾過処理で得られた濾過水１１が処理流量
調整装置５２に供給される。As a result, the raw water pump 8 is turned on, and the turbidity pretreatment unit 7 causes the raw water 2 to be treated.
Of the turbidity components, and after removing large turbidity components, the raw water 2 from which the turbidity components have been removed is supplied to the membrane module 10 to remove organic substances and the like from the raw water 2. The filtered water 11 obtained by this membrane filtration process is supplied to the process flow rate adjusting device 52.

【０１１９】そして、処理流量調整装置５２の流量調整
弁１２によって、濾過モジュール１０から送出される濾
過水１１の流量が調整されながら、濾過水流量計１３に
よって、濾過水１１の流量が測定され、流量検知信号が
膜濾過制御装置５７に供給されるとともに、流量測定済
みの濾過水１１が濾過水タンク５８に一時貯留され、次
の処理に送出される。Then, the flow rate of the filtered water 11 sent from the filtration module 10 is adjusted by the flow rate adjusting valve 12 of the processing flow rate adjusting device 52, and the flow rate of the filtered water 11 is measured by the filtered water flow meter 13. The flow rate detection signal is supplied to the membrane filtration control device 57, and the filtered water 11 whose flow rate has been measured is temporarily stored in the filtered water tank 58 and sent to the next process.

【０１２０】この後、膜濾過処理を開始してから、予め
設定された所定時間が経過すると、膜濾過制御装置５７
によって、膜濾過処理の停止指示が生成されて、膜濾過
装置５１の原水ポンプ８に対するポンプオン信号の出力
が停止するとともに、バルブ閉を示すバルブ開度指定信
号が生成されて、処理流量調整装置５２の流量調整弁１
２がバルブ閉状態にされ、これら膜濾過装置５１、処理
流量調整装置５２の膜濾過処理が停止する。After this, when a predetermined time set in advance has elapsed since the start of the membrane filtration process, the membrane filtration controller 57.
As a result, an instruction to stop the membrane filtration process is generated, the output of the pump-on signal to the raw water pump 8 of the membrane filtration device 51 is stopped, and a valve opening degree designation signal indicating valve closing is generated, and the processing flow rate adjusting device 52 is generated. Flow control valve 1
The valve 2 is closed, and the membrane filtration process of the membrane filtration device 51 and the treatment flow rate adjustment device 52 is stopped.

【０１２１】次いで、膜濾過装置５１、処理流量調整装
置５２の膜濾過処理が完全に停止すると、膜濾過制御装
置５７によって、物理洗浄処理が開始されて、バルブ開
指示信号が生成され、これが洗浄水供給装置５４の逆洗
弁６０、洗浄排水濁度検知装置５６のドレン弁６２に供
給されて、これら逆洗弁６０、ドレン弁６２のバルブが
開状態にされるとともに、洗浄水供給装置５４の逆洗弁
６０から出力されるバルブ開閉検知信号、洗浄排水濁度
検知装置５６のドレン弁６２から出力されるバルブ開閉
検知信号に基づき、逆洗弁６０、ドレン弁６２のバルブ
開閉状態が確認される。Next, when the membrane filtration process of the membrane filtration device 51 and the treatment flow rate adjustment device 52 is completely stopped, the membrane filtration control device 57 starts the physical cleaning process to generate the valve opening instruction signal, which is the cleaning signal. The water is supplied to the backwash valve 60 of the water supply device 54 and the drain valve 62 of the wash drainage turbidity detection device 56, and the valves of the backwash valve 60 and the drain valve 62 are opened, and the wash water supply device 54 is also provided. Check the valve open / close state of the backwash valve 60 and drain valve 62 based on the valve open / close detection signal output from the backwash valve 60 and the valve open / close detection signal output from the drain valve 62 of the cleaning drainage turbidity detector 56. To be done.

【０１２２】この後、膜濾過制御装置５７によって、ポ
ンプオン信号が生成され、これが洗浄水供給装置５４の
逆洗ポンプ５９に供給されて、これがオン状態にされ、
濾過水タンク５８に一時貯留されている濾過水１１の一
部が取り込まれた後、逆洗弁６０を介して、膜モジュー
ル１０の濾過水吐出口から膜モジュール１０の内部に供
給され、膜モジュール１０の逆洗浄が行われるととも
に、この逆洗浄処理で生じた洗浄排水５５が膜モジュー
ル１０の逆洗浄排水口から送出され、洗浄排水濁度検知
装置５６に供給される。Thereafter, the membrane filtration control device 57 generates a pump-on signal, which is supplied to the backwash pump 59 of the wash water supply device 54 to be turned on.
After part of the filtered water 11 temporarily stored in the filtered water tank 58 is taken in, the filtered water is supplied from the filtered water discharge port of the membrane module 10 to the inside of the membrane module 10 via the backwash valve 60. While the backwashing of 10 is performed, the wash drainage 55 generated by this backwashing process is sent out from the backwash drainage port of the membrane module 10 and supplied to the wash drainage turbidity detection device 56.

【０１２３】そして、洗浄排水濁度検知装置５６のドレ
ン弁６２によって、膜濾過装置５１の膜モジュール１０
から送出された逆洗浄排水５５が取り込まれて、排水さ
れるとともに、洗浄排水濁度検知装置５６の濁度計６１
によって、逆洗浄排水５５の濁度が測定され、この測定
動作で得られた濁度検知信号が膜濾過制御装置５７に供
給される。Then, by means of the drain valve 62 of the cleaning wastewater turbidity detection device 56, the membrane module 10 of the membrane filtration device 51.
The backwash drainage 55 sent out from is taken in and drained, and the turbidity meter 61 of the wash drainage turbidity detection device 56 is also included.
Thus, the turbidity of the backwash waste water 55 is measured, and the turbidity detection signal obtained by this measurement operation is supplied to the membrane filtration control device 57.

【０１２４】また、この動作と並行し、膜濾過制御装置
５７によって、逆洗浄処理を開始してからの経過時間
（物理洗浄時間）が測定されるとともに、洗浄排水濁度
検知装置５６の濁度計６１から出力される濁度検知信号
の値（実濁度）と、予め設定されている洗浄完了決定濁
度とが比較され、図１１の洗浄時間／物理洗浄排水濁度
テーブル６２に示すように、予め設定されている物理洗
浄時間が経過したとき、あるいは洗浄排水濁度検知装置
５６の濁度計６１から出力される濁度検知信号の値（実
濁度）が予め設定されている洗浄完了決定濁度より小さ
くなったとき、逆洗洗浄完了と判定されて、洗浄水供給
装置５４の逆洗ポンプ５９に対するポンプオン信号の出
力が停止するとともに、バルブ開指示信号の生成が停止
されて、洗浄水供給装置５４の逆洗弁６０、洗浄排水濁
度検知装置５６のドレン弁６２が閉状態にされ、これら
洗浄水供給装置５４、洗浄排水濁度検知装置５６による
逆洗浄処理が停止する。Further, in parallel with this operation, the membrane filtration control device 57 measures the elapsed time (physical cleaning time) from the start of the reverse cleaning process, and the turbidity of the cleaning drainage turbidity detection device 56. The value of the turbidity detection signal output from the total 61 (actual turbidity) is compared with the preset cleaning completion determination turbidity, and as shown in the cleaning time / physical cleaning drainage turbidity table 62 of FIG. In addition, when the preset physical cleaning time has elapsed, or the value of the turbidity detection signal (actual turbidity) output from the turbidity meter 61 of the cleaning wastewater turbidity detection device 56 is set in advance. When the turbidity becomes smaller than the completion determination turbidity, it is determined that the backwash cleaning is completed, the output of the pump-on signal to the backwash pump 59 of the wash water supply device 54 is stopped, and the generation of the valve opening instruction signal is stopped. Wash water supply Reversing valve 60 of the location 54, drain valve 62 of the washing wastewater turbidity sensing device 56 is in the closed state, these washing water supply device 54, the reverse cleaning with detergent drain turbidity sensing device 56 is stopped.

【０１２５】次いで、洗浄水供給装置５４、洗浄排水濁
度検知装置５６による逆洗浄処理が完全に停止すると、
膜濾過制御装置５７によって、上述した膜濾過処理が再
開されて、原水２の膜濾過処理が行われる。Next, when the backwash process by the wash water supply device 54 and the wash drainage turbidity detection device 56 is completely stopped,
The membrane filtration controller 57 restarts the membrane filtration process described above to perform the membrane filtration process of the raw water 2.

【０１２６】このように、この第５実施形態では、所定
時間毎に、膜濾過装置５１の膜モジュール１０を逆洗浄
して、洗浄排水５５の濁度が所定の濁度以下になるよう
にしながら、処理対象となる原水２を取り込ませて、膜
濾過処理を行わせ、これによって得られた濾過水１１を
次の処理に送水するようにした。As described above, in the fifth embodiment, the membrane module 10 of the membrane filtration device 51 is back-washed every predetermined time so that the turbidity of the cleaning waste water 55 becomes equal to or less than the predetermined turbidity. Then, the raw water 2 to be treated was taken in to perform the membrane filtration treatment, and the filtered water 11 thus obtained was sent to the next treatment.

【０１２７】このため、膜モジュール１０を逆洗浄した
ときに排出される洗浄排水５５の濁度に基づき、膜モジ
ュール１０に対する逆洗浄の終了時期を最適化し、これ
によって膜間差圧上昇を抑えつつ、物理洗浄の回数、薬
品洗浄の回数、濾過膜の交換回数を低減して、システム
の運転コストを低く抑えることができるとともに、膜処
理水量を多くして、システム稼働率を高くすることがで
きる。Therefore, based on the turbidity of the cleaning drainage 55 discharged when the membrane module 10 is backwashed, the end time of the backwashing of the membrane module 10 is optimized, thereby suppressing an increase in transmembrane pressure difference. The number of times of physical cleaning, the number of times of chemical cleaning, and the number of times of exchanging filtration membranes can be reduced to reduce the operating cost of the system, and the amount of membrane-treated water can be increased to increase the system operating rate. .

【０１２８】[0128]

【発明の効果】以上説明したように本発明によれば、シ
ステムの運転コストを低く抑えすることができるととも
に、膜処理水量を多くして、システム稼働率を高くする
ことができる膜濾過システムを提供することができる。As described above, according to the present invention, it is possible to reduce the operating cost of the system, increase the amount of membrane-treated water, and increase the system operation rate. Can be provided.

【図面の簡単な説明】[Brief description of drawings]

【図１】第１実施形態を示すブロック図である。FIG. 1 is a block diagram showing a first embodiment.

【図２】第１実施形態の膜濾過時間／膜間差圧グラフの
一例を示す図である。FIG. 2 is a diagram showing an example of a membrane filtration time / membrane pressure difference graph of the first embodiment.

【図３】第１実施形態の膜間差圧上昇率／膜濾過水流量
グラフの一例を示す図である。FIG. 3 is a diagram showing an example of a transmembrane pressure difference increase rate / membrane filtered water flow rate graph of the first embodiment.

【図４】第１実施形態の膜濾過水流量目標値／原水蛍光
強度テーブルの一例を示す図である。FIG. 4 is a diagram showing an example of a membrane filtration water flow rate target value / raw water fluorescence intensity table according to the first embodiment.

【図５】第２実施形態を示すブロック図である。FIG. 5 is a block diagram showing a second embodiment.

【図６】第３実施形態を示すブロック図である。FIG. 6 is a block diagram showing a third embodiment.

【図７】第３実施形態の膜濾過時間／膜間差圧グラフの
一例を示す図である。FIG. 7 is a diagram showing an example of a membrane filtration time / membrane pressure difference graph of the third embodiment.

【図８】第３実施形態の膜間差圧上昇率／膜濾過水流量
グラフの一例を示す図である。FIG. 8 is a diagram showing an example of a transmembrane pressure difference increase rate / membrane filtered water flow rate graph of a third embodiment.

【図９】第３実施形態の膜濾過水流量目標値／原水吸光
度テーブルの一例を示す模式図である。FIG. 9 is a schematic diagram showing an example of a membrane filtered water flow rate target value / raw water absorbance table according to the third embodiment.

【図１０】第５実施形態を示すブロック図である。FIG. 10 is a block diagram showing a fifth embodiment.

【図１１】第５実施形態の洗浄時間／物理洗浄排水濁度
テーブルの一例を示す図である。FIG. 11 is a diagram showing an example of a cleaning time / physical cleaning wastewater turbidity table of the fifth embodiment.

【符号の説明】[Explanation of symbols]

１ａ〜１ｄ：膜濾過システム ２：原水 ３、３１、５１：膜濾過装置 ４：処理流量調整装置 ５：膜濾過水流量目標値演算装置（膜濾過制御装置） ６：流量一定制御装置（膜濾過制御装置） ７：除濁用前処理器 ８：原水ポンプ ９：蛍光分析計（原水蛍光分析計） １０：膜モジュール １１：濾過水 １２：流量調整弁 １３：濾過水流量計 １４、３４：膜濾過水流量目標値／原水蛍光強度テーブ
ル ２１、５２：処理流量調整装置 ２２、３２：膜濾過水流量目標値演算装置（膜濾過制御
装置） ２３：蛍光分析計（濾過水蛍光分析計） ３３：吸光度計（原水吸光度計） ５３：洗浄水 ５４：洗浄水供給装置 ５５：洗浄排水 ５６：洗浄排水濁度検知装置 ５７：膜濾過制御装置 ５８：濾過水タンク ５９：逆洗ポンプ ６０：逆洗弁 ６１：濁度計（洗浄排水濁度計） ６２：ドレン弁1a to 1d: Membrane filtration system 2: Raw water 3, 31, 51: Membrane filtration device 4: Treatment flow rate adjusting device 5: Membrane filtration water flow rate target value calculation device (membrane filtration control device) 6: Constant flow rate control device (membrane filtration Control device) 7: Pretreatment device for decontamination 8: Raw water pump 9: Fluorescence analyzer (raw water fluorescence analyzer) 10: Membrane module 11: Filtered water 12: Flow control valve 13: Filtered water flow meters 14, 34: Membrane Filtered water flow rate target value / raw water fluorescence intensity table 21, 52: Treatment flow rate adjusting devices 22, 32: Membrane filtered water flow rate target value calculation device (membrane filtration control device) 23: Fluorescence analyzer (filtered water fluorescence analyzer) 33: Absorbance meter (raw water absorbance meter) 53: Wash water 54: Wash water supply device 55: Wash drain 56: Wash drain turbidity detector 57: Membrane filtration controller 58: Filter water tank 59: Backwash pump 60: Backwash valve 61: Turbidimeter (washing wastewater turbidimeter 62: Drain valve

───────────────────────────────────────────────────── フロントページの続き (72)発明者 居安 巨太郎 東京都府中市東芝町１番地 株式会社東芝 府中事業所内 (72)発明者 竹内 賢治 東京都府中市東芝町１番地 株式会社東芝 府中事業所内 (72)発明者 川路 等 東京都府中市東芝町１番地 株式会社東芝 府中事業所内 (72)発明者 内田 祥司 東京都港区芝浦一丁目１番１号 株式会社 東芝本社事務所内 (72)発明者 金元 幹男 東京都港区芝浦一丁目１番１号 株式会社 東芝本社事務所内 Ｆターム(参考） 2G043 AA01 BA14 CA03 DA05 EA01 EA13 JA01 KA02 KA05 LA01 NA01 2G059 AA01 AA02 BB05 CC12 CC19 DD12 EE01 EE02 HH03 HH06 MM01 MM05 PP10 4D006 GA02 KA02 KB14 KC03 KE02Q KE12P KE13P KE25Q PB08   ─────────────────────────────────────────────────── ─── Continued front page    (72) Inventor Gitaro Iyasu             No. 1 Toshiba-cho, Fuchu-shi, Tokyo Toshiba Corporation             Fuchu Office (72) Inventor Kenji Takeuchi             No. 1 Toshiba-cho, Fuchu-shi, Tokyo Toshiba Corporation             Fuchu Office (72) Inventor Kawaji, etc.             No. 1 Toshiba-cho, Fuchu-shi, Tokyo Toshiba Corporation             Fuchu Office (72) Inventor Shoji Uchida             1-1 Shibaura, Minato-ku, Tokyo Co., Ltd.             Toshiba headquarters office (72) Inventor Mikio Kanemoto             1-1 Shibaura, Minato-ku, Tokyo Co., Ltd.             Toshiba headquarters office F term (reference) 2G043 AA01 BA14 CA03 DA05 EA01                       EA13 JA01 KA02 KA05 LA01                       NA01                 2G059 AA01 AA02 BB05 CC12 CC19                       DD12 EE01 EE02 HH03 HH06                       MM01 MM05 PP10                 4D006 GA02 KA02 KB14 KC03 KE02Q                       KE12P KE13P KE25Q PB08

Claims (12)

【特許請求の範囲】[Claims] 【請求項１】 膜モジュールを使用して原水の水質を改
善する膜濾過システムにおいて、 前記膜モジュールに供給される前記原水の蛍光強度を測
定する原水蛍光分析計と、 この原水蛍光分析計の測定結果に基づき、前記膜モジュ
ールで膜濾過処理される原水の流量を制御する膜濾過制
御装置と、 を備えたことを特徴とする膜濾過システム。1. A membrane filtration system for improving the water quality of raw water using a membrane module, comprising: a raw water fluorescence analyzer for measuring the fluorescence intensity of the raw water supplied to the membrane module; and a measurement of the raw water fluorescence analyzer. A membrane filtration control device that controls the flow rate of raw water that is subjected to membrane filtration in the membrane module based on the result, and a membrane filtration system. 【請求項２】 請求項１に記載の膜濾過システムにおい
て、 前記膜モジュールに供給される前記原水の濁度を測定す
る原水濁度計を備え、前記膜濾過制御装置は、原水濁度
計の測定結果と原水蛍光分析計の測定結果に基づいて前
記膜モジュールで膜濾過処理される原水の流量を制御す
る、 ことを特徴とする膜濾過システム。2. The membrane filtration system according to claim 1, further comprising a raw water turbidity meter for measuring the turbidity of the raw water supplied to the membrane module, wherein the membrane filtration control device is a raw water turbidity meter. A membrane filtration system, wherein the flow rate of raw water subjected to membrane filtration in the membrane module is controlled based on the measurement result and the measurement result of the raw water fluorescence analyzer. 【請求項３】 請求項１、２のいずれかに記載の膜濾過
システムにおいて、 前記膜モジュールから送出される濾過水の蛍光強度を測
定する濾過水蛍光分析計を備え、前記膜濾過制御装置
は、濾過水蛍光分析計の測定結果と原水蛍光分析計の測
定結果に基づいて前記膜モジュールで膜濾過処理される
原水の流量を制御する、 ことを特徴とする膜濾過システム。3. The membrane filtration system according to claim 1, further comprising a filtered water fluorescence analyzer for measuring a fluorescence intensity of filtered water delivered from the membrane module, wherein the membrane filtration control device comprises: A membrane filtration system, wherein the flow rate of raw water subjected to membrane filtration in the membrane module is controlled based on the measurement result of the filtered water fluorescence analyzer and the measurement result of the raw water fluorescence analyzer. 【請求項４】 請求項１乃至３のいずれかに記載の膜濾
過システムにおいて、 前記膜濾過制御装置は、前記濾過水蛍光分析計の測定結
果、前記原水蛍光分析計の測定結果のうち、少なくとも
いずれか一方または組み合わせ内容に基づいて前記膜モ
ジュールに対する逆洗浄開始時期を制御する、 ことを特徴とする膜濾過システム。4. The membrane filtration system according to claim 1, wherein the membrane filtration controller is at least one of a measurement result of the filtered water fluorescence analyzer and a measurement result of the raw water fluorescence analyzer. A membrane filtration system, characterized in that the start time of backwashing for the membrane module is controlled based on either one or the combination content. 【請求項５】 請求項１乃至４のいずれかに記載の膜濾
過システムにおいて、 前記濾過水蛍光分析計、前記原水蛍光分析計のうち、少
なくともいずれか一方は、波長“３４０〜３５０ｎｍ”
の間にある特定波長の励起光と、波長“４２０〜４３０
ｎｍ”の間にある特定の蛍光を使用して原水または濾過
水の蛍光強度を測定する、 ことを特徴とする膜濾過システム。5. The membrane filtration system according to claim 1, wherein at least one of the filtered water fluorescence analyzer and the raw water fluorescence analyzer has a wavelength of “340 to 350 nm”.
Of excitation light of a specific wavelength between the wavelengths of "420 to 430
A membrane filtration system, characterized in that the fluorescence intensity of the raw water or the filtered water is measured using a specific fluorescence lying between nm ". 【請求項６】 膜モジュールを使用して原水の水質を改
善する膜濾過システムにおいて、 前記膜モジュールに供給される原水の吸光度を測定する
原水吸光度計と、 この原水吸光度計の測定結果に基づいて前記膜モジュー
ルで膜濾過処理される原水の流量を制御する膜濾過制御
装置と、 を備えたことを特徴とする膜濾過システム。6. A membrane filtration system for improving the quality of raw water using a membrane module, comprising: a raw water absorbance meter for measuring the absorbance of raw water supplied to the membrane module; and a measurement result of the raw water absorbance meter. A membrane filtration control device that controls the flow rate of raw water that is subjected to membrane filtration in the membrane module. 【請求項７】 請求項１、６に記載の膜濾過システムに
おいて、 前記膜モジュールに供給される前記原水の濁度を測定す
る原水濁度計を備え、前記膜濾過制御装置は、原水濁度
計の測定結果と前記原水吸光度計の測定結果に基づいて
前記膜モジュールで膜濾過処理される原水の流量を制御
する、 ことを特徴とする膜濾過システム。7. The membrane filtration system according to claim 1, further comprising a raw water turbidity meter for measuring the turbidity of the raw water supplied to the membrane module, wherein the membrane filtration control device has a raw water turbidity. A membrane filtration system, wherein a flow rate of raw water subjected to membrane filtration in the membrane module is controlled based on a measurement result of a meter and a measurement result of the raw water absorbance meter. 【請求項８】 請求項６、７のいずれかに記載の膜濾過
システムにおいて、 前記膜モジュールから送出される濾過水の吸光度を測定
する濾過水吸光度計を備え、前記膜濾過制御装置は、濾
過水吸光度計の測定結果と前記原水吸光度計の測定結果
に基づいて前記膜モジュールで膜濾過処理される原水の
流量を制御する、 ことを特徴とする膜濾過システム。8. The membrane filtration system according to claim 6, further comprising a filtered water absorptiometer for measuring an absorbance of filtered water delivered from the membrane module, wherein the membrane filtration control device comprises a filtration unit. A membrane filtration system, wherein the flow rate of raw water subjected to membrane filtration in the membrane module is controlled based on a measurement result of a water absorbance meter and a measurement result of the raw water absorbance meter. 【請求項９】 請求項６乃至８のいずれかに記載の膜濾
過システムにおいて、 前記膜濾過制御装置は、前記濾過水吸光度計の測定結
果、前記原水吸光度計の測定結果のうち、少なくともい
ずれか一方、または組み合わせ内容に基づいて前記膜モ
ジュールに対する逆洗浄開始時期を制御する、 ことを特徴とする膜濾過システム。9. The membrane filtration system according to claim 6, wherein the membrane filtration controller is at least one of a measurement result of the filtered water absorbance meter and a measurement result of the raw water absorbance meter. On the other hand, the membrane filtration system is characterized in that the backwash start timing for the membrane module is controlled based on the content of the combination. 【請求項１０】 請求項６乃至９のいずれかに記載の膜
濾過システムにおいて、 前記濾過水吸光度計、前記原水吸光度計のうち、少なく
ともいずれか一方は、波長“２５０〜２７０ｎｍ”の間
にある特定波長の光に対する吸光度を使用して原水また
は濾過水の吸光度を測定する、 ことを特徴とする膜濾過システム。10. The membrane filtration system according to claim 6, wherein at least one of the filtered water absorptiometer and the raw water absorptiometer is in a wavelength range of “250 to 270 nm”. A membrane filtration system, characterized in that the absorbance of raw water or filtered water is measured using the absorbance for light of a specific wavelength. 【請求項１１】 請求項６乃至１０のいずれかに記載の
膜濾過システムにおいて、 前記濾過水吸光度計、前記原水吸光度計のうち、少なく
ともいずれか一方は、波長“３８０〜４００ｎｍ”の間
にある特定波長の光に対する吸光度を使用して原水また
は濾過水の吸光度を測定する、 ことを特徴とする膜濾過システム。11. The membrane filtration system according to claim 6, wherein at least one of the filtered water absorptiometer and the raw water absorptiometer is in a wavelength range of “380 to 400 nm”. A membrane filtration system, characterized in that the absorbance of raw water or filtered water is measured using the absorbance for light of a specific wavelength. 【請求項１２】 請求項１乃至１１のいずれかに記載の
膜濾過システムにおいて、 前記膜濾過制御装置は、前記膜モジュールに対する逆洗
浄処理から排出される洗浄排水の濁度を測定する洗浄排
水濁度計の測定結果、または前記洗浄排水の蛍光強度を
測定する洗浄水蛍光分析計の測定結果、あるいは前記洗
浄排水の吸光度を測定する洗浄水吸光度計の測定結果の
いずれかに基づき、前記膜モジュールに対する逆洗浄終
了時期を制御する、 ことを特徴とする膜濾過システム。12. The membrane filtration system according to claim 1, wherein the membrane filtration control device measures the turbidity of the cleaning wastewater discharged from the backwashing process for the membrane module. The membrane module based on either the measurement result of a spectrophotometer, the measurement result of a wash water fluorescence analyzer for measuring the fluorescence intensity of the washing wastewater, or the measurement result of a wash water spectrophotometer for measuring the absorbance of the washing wastewater. The membrane filtration system is characterized in that it controls the end time of backwashing.
JP2001329474A 2001-10-26 2001-10-26 Membrane filter system Pending JP2003126855A (en)

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