JP2008194560A - Evaluation method of water to be treated in membrane separation device, water treatment method, and water treatment device - Google Patents
Evaluation method of water to be treated in membrane separation device, water treatment method, and water treatment device Download PDFInfo
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- Separation Using Semi-Permeable Membranes (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Physical Water Treatments (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Water Treatment By Sorption (AREA)
Abstract
Description
本発明は、膜分離装置に供給される被処理水の評価方法、被処理水を膜分離装置で膜分離処理して濃縮水と透過水とに分離する水処理方法及び水処理装置に関する。 The present invention relates to a method for evaluating water to be treated supplied to a membrane separation device, a water treatment method and a water treatment device for separating water to be treated into a concentrated water and a permeated water by membrane separation treatment with the membrane separation device.
なお、本発明において、「逆浸透膜」は、「逆浸透膜」と「ナノ濾過膜」を包含する広義の「逆浸透膜」を意味する。 In the present invention, “reverse osmosis membrane” means “reverse osmosis membrane” in a broad sense including “reverse osmosis membrane” and “nanofiltration membrane”.
I. 逆浸透膜は溶質の阻止率が高いため、逆浸透膜処理により得られる透過水は良好な水質を有するので、各種用途に有効に再利用が可能である。しかし、その一方で、処理の継続に伴い膜の透過流束が低下し、操作圧力が上昇するため、この場合には、膜性能を回復させるために、運転を停止して逆浸透膜を洗浄する処理が必要となる。 I. Since the reverse osmosis membrane has a high solute rejection rate, the permeated water obtained by the reverse osmosis membrane treatment has good water quality and can be effectively reused in various applications. However, on the other hand, the permeation flux of the membrane decreases with the continuation of the process and the operating pressure increases. In this case, the operation is stopped and the reverse osmosis membrane is washed to restore the membrane performance. It is necessary to perform processing.
(i) 従来においては、逆浸透膜を用いて水処理を行う場合、このような膜洗浄頻度を低減して、処理効率を高めるために、逆浸透膜モジュールへの供給水を、JIS K3802に定義されているファウリングインデックス(FI)、又はASTM D4189に定義されているシルトデンシティインデックス(SDI)や、より簡便な評価方法として谷口により提案されたMF値(Desalination,vol.20,p.353−364,1977)で評価し、この値が既定値以下となるように、例えばFI値又はSDI値が3〜4、あるいはそれ以下となるように、必要に応じて前処理を実施し、逆浸透膜供給水をある程度清澄にすることにより、逆浸透膜モジュールにおける透過流束の低下や操作圧力の上昇などの障害を避け、安定運転を継続する方法が実施されている。 (I) Conventionally, when water treatment is performed using a reverse osmosis membrane, water supplied to the reverse osmosis membrane module is supplied to JIS K3802 in order to reduce the frequency of such membrane cleaning and increase the treatment efficiency. Defined fouling index (FI), silt density index (SDI) defined in ASTM D4189, and MF value proposed by Taniguchi as a simpler evaluation method (Desalination, vol. 20, p.353) -364, 1977), pre-processing is performed as necessary so that this value is less than the predetermined value, for example, the FI value or SDI value is 3 to 4, or less. By clarifying the osmosis membrane supply water to some extent, obstacles such as a decrease in permeation flux and an increase in operating pressure in the reverse osmosis membrane module are avoided. , How to continue the stable operation is performed.
FI値、SDI値、MF値はいずれも逆浸透膜供給水を0.45μmの精密濾過膜(通常、日本ミリポア株式会社の「ミリポアフィルター」を用いることが多い。)で濾過したときの所定の濾過時間を測定し、この測定値に基いて算出されるものである。前処理としては、例えば、工場廃水の場合、活性汚泥法などによる生物学的処理や、活性炭吸着、限外濾過などの物理化学的処理を行うことが一般的である。 The FI value, SDI value, and MF value are all determined when the reverse osmosis membrane feed water is filtered through a 0.45 μm microfiltration membrane (usually, a “Millipore filter” manufactured by Nihon Millipore Corporation is often used). The filtration time is measured and calculated based on this measured value. As the pretreatment, for example, in the case of factory wastewater, it is common to perform biological treatment by an activated sludge method or the like, or physicochemical treatment such as activated carbon adsorption or ultrafiltration.
しかしながら、FI値又はSDI値やMF値が既定値以下の逆浸透膜供給水であっても、逆浸透膜において透過流束の低下や操作圧力の上昇が早期に発生する場合があった。即ち、従来のFI値、SDI値又はMF値の評価は、逆浸透膜供給水中のSS(懸濁固形物)を捕捉することにより、これを濾過時間に反映することができるため、SSに基く逆浸透膜供給水としての良否の判定には有効であるが、原水中の溶解性の汚れ成分を濾過時間に反映しない。このため、溶存物質の化学的相互作用に基く逆浸透膜供給水としての良否を的確には判定できない。 However, even if the reverse osmosis membrane supply water has a FI value, an SDI value, or an MF value equal to or lower than a predetermined value, a decrease in permeation flux and an increase in operating pressure may occur at an early stage in the reverse osmosis membrane. That is, the conventional evaluation of FI value, SDI value or MF value is based on SS because it can be reflected in filtration time by capturing SS (suspended solids) in reverse osmosis membrane feed water. Although effective for determining the quality of the reverse osmosis membrane supply water, the soluble soil component in the raw water is not reflected in the filtration time. For this reason, the quality as reverse osmosis membrane supply water based on the chemical interaction of dissolved substances cannot be accurately determined.
(ii) 特開2004−188387号公報では、逆浸透膜供給水をポリアミド系メンブレンフィルターに通水し、濾過抵抗の大小により逆浸透膜供給水としての良否を評価する方法が示されている。この方法であれば、逆浸透膜と同素材のポリアミド系メンブレンフィルターを用いることにより、供給水中に溶存し、逆浸透膜に吸着して障害となるような膜汚染物質も検出することができる。しかしながら、ポリアミド系メンブレンフィルターは精密濾過膜であり、いかに逆浸透膜と素材が同一であったとしても、逆浸透膜における透過流束の低下等を予測するには限界があり、必ずしも十分な逆浸透膜供給水の管理ができるわけではない。また、評価操作自体も煩雑で手間を要するという不具合があった。 (Ii) Japanese Patent Application Laid-Open No. 2004-188387 discloses a method in which reverse osmosis membrane supply water is passed through a polyamide membrane filter, and the quality of the reverse osmosis membrane supply water is evaluated based on the magnitude of filtration resistance. With this method, by using a polyamide membrane filter made of the same material as the reverse osmosis membrane, it is also possible to detect a membrane contaminant that dissolves in the supply water and adsorbs on the reverse osmosis membrane. However, polyamide membrane filters are microfiltration membranes, and no matter how the reverse osmosis membrane and the material are the same, there is a limit to predicting a decrease in the permeation flux in the reverse osmosis membrane. Management of osmotic membrane feed water is not possible. In addition, the evaluation operation itself is complicated and troublesome.
(iii) 特開平10−286445号公報では、分離膜供給水を主膜モジュールと主膜モジュールよりも小さな膜面積を有する副膜モジュールに通水し、主膜モジュールと副膜モジュールの動作状態を対比することにより、主膜モジュール又は副膜モジュール、或いはその両方における透過水量の低下が、膜分離装置の原水に起因するものか、機器自体に起因するものかを判別する方法が示されている。しかしながら、この方法は、主膜モジュール又は副膜モジュール、或いは両方のモジュールにおいて発生した透過水量の低下が、膜供給水水質の悪化によるものか、装置の不備によるものかを判別する手法であり、必ずしも膜供給水の水質の良否を判断する方法ではない。 (Iii) In Japanese Patent Laid-Open No. 10-286445, separation membrane feed water is passed through a main membrane module and a sub-membrane module having a membrane area smaller than that of the main membrane module, and the operation state of the main membrane module and the sub-membrane module is changed. By contrast, a method for determining whether the decrease in the amount of permeated water in the main membrane module or the sub-membrane module or both is caused by the raw water of the membrane separation apparatus or the device itself is shown. . However, this method is a method for discriminating whether the decrease in the amount of permeated water generated in the main membrane module or the sub-membrane module or both modules is due to deterioration in the quality of the water supplied to the membrane or due to inadequate equipment. It is not necessarily a method for judging the quality of the water supplied to the membrane.
仮にこの方法を逆浸透膜供給水の評価に用いようとした場合、主膜モジュールと副膜モジュールともに連続的に長期通水するので、副膜モジュールにおいて透過流束の低下を検知したときには既に主膜モジュールにおいても透過水量が低下していることとなる。逆浸透膜においては、一度透過水量が低下してしまうと薬品洗浄等でもなかなか回復できないような不可逆な汚染も発生することから、この方法では手遅れとなってしまう。 If this method is to be used for the evaluation of reverse osmosis membrane feed water, both the main membrane module and the sub membrane module continuously pass water for a long time. Even in the membrane module, the amount of permeated water is reduced. In a reverse osmosis membrane, once the permeated water amount is reduced, irreversible contamination that cannot be easily recovered by chemical cleaning or the like is generated, so this method is too late.
しかも、膜モジュールに連続的に通水する場合、主膜モジュール、副膜モジュールにおいて透過水量の低下を検出した時点における供給水は必ずしも悪化しているとは限らない。一方で、逆浸透膜供給水が例えば排水等の場合、水質は刻一刻と変化しており、その時点における即時的な水質の評価が必要とされるが、膜モジュールに供給水を連続通水する特開平10−286445号公報の方法では、どの時期で透過水量が低下したのかを判定することはできず、その時々の供給水の水質を十分に評価することはできない。 Moreover, when water is continuously passed through the membrane module, the supply water at the time when the decrease in the amount of permeated water is detected in the main membrane module and the sub membrane module is not necessarily deteriorated. On the other hand, when the reverse osmosis membrane supply water is, for example, drainage, the water quality is changing every moment, and an immediate evaluation of the water quality is required at that time, but the supply water is continuously passed through the membrane module. In the method disclosed in Japanese Patent Laid-Open No. 10-286445, it is impossible to determine at which time the amount of permeated water has decreased, and the quality of the supplied water at that time cannot be sufficiently evaluated.
(iv) 特開2005−103431号公報には、逆浸透膜装置(以下「主逆浸透膜装置」と称す。)に供給される水の逆浸透膜供給水としての良否を、該逆浸透膜装置の運転中に評価する方法であって、該主逆浸透膜装置とは別の評価用逆浸透膜装置に該逆浸透膜供給水を断続的に通水し、該評価用逆浸透膜装置における通水開始後所定時間内の逆浸透膜供給水の透過性を測定し、この測定値を予め設定した基準値と比較することにより、該逆浸透膜供給水を評価する方法が示されている。 (Iv) In Japanese Patent Application Laid-Open No. 2005-103431, the quality of water supplied to a reverse osmosis membrane device (hereinafter referred to as “main reverse osmosis membrane device”) is determined as the reverse osmosis membrane supply water. A method of evaluation during operation of the apparatus, wherein the reverse osmosis membrane supply water is intermittently passed through an evaluation reverse osmosis membrane apparatus different from the main reverse osmosis membrane apparatus, and the evaluation reverse osmosis membrane apparatus Shows a method for evaluating the reverse osmosis membrane feed water by measuring the permeability of the reverse osmosis membrane feed water within a predetermined time after the start of water flow and comparing the measured value with a preset reference value. Yes.
この方法によれば、逆浸透膜供給水を評価用逆浸透膜装置に断続的に通水し、その通水初期の所定時間内の逆浸透膜供給水の透過性、特に透過水量を基準値と比較することにより、逆浸透膜供給水としての良否を、短時間で簡易に、正確に評価することができる。 According to this method, the reverse osmosis membrane feed water is intermittently passed through the evaluation reverse osmosis membrane device, and the permeability of the reverse osmosis membrane feed water within a predetermined time at the initial stage of the water flow, particularly the permeated water amount, is a reference value. As a result, it is possible to simply and accurately evaluate the quality of the reverse osmosis membrane supply water in a short time.
しかしながら、この方法は、逆浸透膜に供給水を通水し、その透水性によって給水を評価するものであるため、汚染の程度の大きい給水については精度よく評価できるものの、汚染の程度の比較的小さい給水の評価を精度よく行うことができない。また、主逆浸透装置とは別に評価用逆浸透膜装置を設ける必要があり、装置が複雑化及び大型化する。さらに、この方法では評価用逆浸透膜装置に比較的多量の逆浸透膜供給水を通水する必要があり、通水に時間がかかることから、評価に時間がかかる。
II. 半導体・液晶などの電子デバイス製造工場において、回収された電子デバイスの洗浄排水の水処理に、純水製造装置が用いられている。この純水製造装置内においても、塩類や有機物質(TOC)を除去するための装置として、逆浸透膜(RО)装置が用いられている。
However, in this method, since the feed water is passed through the reverse osmosis membrane and the water supply is evaluated by the water permeability, the water supply with a high degree of contamination can be evaluated accurately, but the contamination level is relatively high. Small water supply cannot be evaluated accurately. Moreover, it is necessary to provide a reverse osmosis membrane device for evaluation separately from the main reverse osmosis device, which complicates and enlarges the device. Furthermore, in this method, it is necessary to pass a relatively large amount of reverse osmosis membrane feed water through the evaluation reverse osmosis membrane device, and it takes time to pass the water.
II. In an electronic device manufacturing factory for semiconductors and liquid crystals, a pure water manufacturing apparatus is used for water treatment of the washed waste water of the collected electronic devices. Also in this pure water production apparatus, a reverse osmosis membrane (RO) apparatus is used as an apparatus for removing salts and organic substances (TOC).
近年、これらの工場における非イオン界面活性剤の使用量が増加しており、これに伴い、非イオン界面活性剤の純水製造装置内への流入量も増加している。非イオン界面活性剤が逆浸透膜装置に供給されると、微量濃度であっても逆浸透膜が著しく汚染され、逆浸透膜装置の水処理量が著しく低下する。このため、逆浸透膜装置の上流にオゾン酸化塔や活性炭吸着塔などを設置し、非イオン界面活性剤の分解や吸着除去を行うことにより、この水処理量の低下の抑制が図られている。 In recent years, the amount of nonionic surfactants used in these factories has increased, and accordingly, the amount of nonionic surfactants flowing into the pure water production apparatus has also increased. When the nonionic surfactant is supplied to the reverse osmosis membrane device, the reverse osmosis membrane is significantly contaminated even at a very small concentration, and the amount of water treated by the reverse osmosis membrane device is significantly reduced. For this reason, an ozone oxidation tower, an activated carbon adsorption tower, etc. are installed upstream of the reverse osmosis membrane device, and the reduction of this water treatment amount is suppressed by decomposing and removing the nonionic surfactant. .
この純水製造装置を運転する際には、逆浸透膜装置に供給される被処理水の比抵抗や有機物質(TOC)濃度を測定し、この測定結果に基づいて運転管理が行われる。
上記の通り、逆浸透膜装置で被処理水を水処理する場合、逆浸透膜装置に供給される被処理水自体の水質を測定し、この測定結果に基づいて被処理水の水質評価を行っている。このため、以下に説明する通り、被処理水の水質評価に時間がかかる、被処理水中に含まれる微量の膜ファウリング物質を検出することが困難である、という問題がある。 As described above, when water to be treated is treated with a reverse osmosis membrane device, the quality of the water to be treated itself supplied to the reverse osmosis membrane device is measured, and the quality of the water to be treated is evaluated based on the measurement result. ing. For this reason, as described below, there is a problem that it takes time to evaluate the quality of the water to be treated and it is difficult to detect a trace amount of membrane fouling substance contained in the water to be treated.
即ち、上記Iでは、逆浸透膜装置に供給される被処理水の一部を測定用膜に通水し、濾過時間、濾過抵抗又は透過水量の測定結果に基づいて被処理水の評価を行っている。このように、測定用膜に通水する水が逆浸透膜装置に通水する水と同一であるため、測定用膜に膜ファウリング物質が徐々に付着することになり、膜ファウリング物質の検知に時間がかかる。 That is, in I above, a portion of the water to be treated supplied to the reverse osmosis membrane device is passed through the measurement membrane, and the water to be treated is evaluated based on the measurement results of filtration time, filtration resistance or permeated water amount. ing. In this way, since the water flowing through the measurement membrane is the same as the water flowing through the reverse osmosis membrane device, the membrane fouling substance gradually adheres to the measurement membrane, and the membrane fouling substance It takes time to detect.
また、上記IIでは、逆浸透膜装置に供給される被処理水の比抵抗や有機物質(TOC)濃度を測定し、この測定結果に基づいて被処理水の評価を行っている。このため、被処理水中の膜ファウリング物質の含有量が微量であると、該膜ファウリング物質を検知することができない。ところが、被処理水中に含まれる膜ファウリング物質の含有量が微量であったとしても、濃縮水では膜ファウリング物質が濃縮されているため、逆浸透膜のうち濃縮水と接触する側からファウリングが生じることになる。 Moreover, in said II, the specific resistance and organic substance (TOC) density | concentration of the to-be-processed water supplied to a reverse osmosis membrane apparatus are measured, and the to-be-processed water is evaluated based on this measurement result. For this reason, if the content of the membrane fouling substance in the water to be treated is very small, the membrane fouling substance cannot be detected. However, even if the amount of the membrane fouling substance contained in the water to be treated is very small, since the membrane fouling substance is concentrated in the concentrated water, the fouling from the side in contact with the concentrated water in the reverse osmosis membrane. A ring will occur.
例えば、逆浸透膜としてポリアミド系逆浸透膜を用いる場合、このポリアミド系逆浸透膜は、濃度200ppb as TOCのアルキルフェニルエーテル型非イオン界面活性剤に接触すると透過水量が低下する。ここで、逆浸透膜は通常、回収率75〜90%(4倍濃縮〜10倍濃縮)で運転されるため、上記非イオン界面活性剤が被処理水中に20〜50ppb含まれると、濃縮水中の該非イオン界面活性剤濃度が200ppbを超えることになり、逆浸透膜の濃縮水側にファウリングが生じ、逆浸透膜装置の運転に影響が生じるおそれがある。しかしながら、数十ppbレベルの非イオン界面活性剤の測定は非常に難しいため、被処理水の濃度測定を行う場合、この濃度レベルの非イオン界面活性剤を検出することは困難である。 For example, when a polyamide-based reverse osmosis membrane is used as the reverse osmosis membrane, the amount of permeated water decreases when the polyamide-based reverse osmosis membrane comes into contact with an alkylphenyl ether type nonionic surfactant having a concentration of 200 ppb as TOC. Here, since the reverse osmosis membrane is usually operated at a recovery rate of 75 to 90% (4 times concentration to 10 times concentration), when the nonionic surfactant is contained in the water to be treated in an amount of 20 to 50 ppb, the concentration water The concentration of the nonionic surfactant exceeds 200 ppb, and fouling occurs on the concentrated water side of the reverse osmosis membrane, which may affect the operation of the reverse osmosis membrane device. However, since it is very difficult to measure a nonionic surfactant at a level of several tens of ppb, it is difficult to detect a nonionic surfactant at this concentration level when measuring the concentration of water to be treated.
本発明は、膜分離装置に供給される被処理水の水質の評価を高精度で行うことができる膜分離装置被処理水の評価方法と、この評価結果に基づいて運転することにより、分離膜の透過流束の低下を事前に回避し、長期間にわたって膜分離装置を安定して運転することができる水処理方法及び水処理装置を提供することを目的とする。 The present invention provides a method for evaluating the water to be treated to be treated supplied to the membrane separator with high accuracy, and a separation membrane by operating based on the evaluation result. An object of the present invention is to provide a water treatment method and a water treatment apparatus capable of avoiding a decrease in permeation flux in advance and stably operating a membrane separation apparatus over a long period of time.
請求項1の膜分離装置被処理水の評価方法は、膜分離装置に供給される膜ファウリング物質を含む被処理水の水質を評価する方法であって、該膜分離装置からの濃縮水中の膜ファウリング物質濃度を測定し、この測定結果に基づいて該被処理水の水質を評価することを特徴とする。 The method for evaluating treated water of a membrane separation device according to claim 1 is a method for evaluating the quality of treated water containing a membrane fouling substance supplied to the membrane separation device, wherein the water in the concentrated water from the membrane separation device is evaluated. The membrane fouling substance concentration is measured, and the quality of the water to be treated is evaluated based on the measurement result.
請求項2の膜分離装置被処理水の評価方法は、請求項1において、前記濃縮水の蛍光強度を測定することにより、前記濃縮水中の膜ファウリング物質濃度の測定を行うことを特徴とする。 The method for evaluating water to be treated of a membrane separation apparatus according to claim 2 is characterized in that in claim 1, the concentration of membrane fouling substance in the concentrated water is measured by measuring the fluorescence intensity of the concentrated water. .
請求項3の膜分離装置被処理水の評価方法は、請求項1又は2において、前記膜ファウリング物質は非イオン界面活性剤であることを特徴とする。 According to a third aspect of the present invention, there is provided the method for evaluating water to be treated of the membrane separation apparatus according to the first or second aspect, wherein the membrane fouling substance is a nonionic surfactant.
請求項4の膜分離装置被処理水の評価方法は、請求項3において、前記非イオン界面活性剤がアルキルフェニルエーテル型非イオン界面活性剤であり、波長300〜400nmの範囲の蛍光強度を測定することを特徴とする。 The method for evaluating water to be treated of a membrane separation apparatus according to claim 4 is the method according to claim 3, wherein the nonionic surfactant is an alkylphenyl ether type nonionic surfactant, and the fluorescence intensity in the wavelength range of 300 to 400 nm is measured. It is characterized by doing.
請求項5の水処理方法は、膜ファウリング物質を含む被処理水を膜ファウリング物質処理手段で処理した後、膜分離装置で膜分離処理して濃縮水と透過水とに分離する水処理方法において、該膜分離装置からの濃縮水中に含有される膜ファウリング物質濃度を測定し、この測定結果に基づき、前記膜ファウリング物質処理手段を制御することを特徴とする。 The water treatment method according to claim 5 is a water treatment in which water to be treated containing a membrane fouling substance is treated with a membrane fouling substance treatment means, and then separated into concentrated water and permeate by membrane separation treatment with a membrane separator. In the method, the membrane fouling substance concentration contained in the concentrated water from the membrane separation apparatus is measured, and the membrane fouling substance treatment means is controlled based on the measurement result.
請求項6の水処理方法は、請求項5において、前記膜ファウリング物質処理手段は、酸化分解装置、凝集処理装置及び活性炭吸着装置よりなる群から選択される少なくとも1つであることを特徴とする。 The water treatment method of claim 6 is characterized in that, in claim 5, the membrane fouling substance treatment means is at least one selected from the group consisting of an oxidative decomposition apparatus, a coagulation treatment apparatus, and an activated carbon adsorption apparatus. To do.
請求項7の水処理装置は、膜ファウリング物質を含む被処理水が導入される膜ファウリング物質処理手段と、該膜ファウリング物質処理手段で処理された水を膜分離処理して濃縮水と透過水とに分離する膜分離装置と、該膜分離装置からの濃縮水中に含有される膜ファウリング物質の濃度を測定する膜ファウリング物質濃度測定手段と、この膜ファウリング物質濃度測定手段の測定結果に基づき、前記膜ファウリング物質処理手段を制御する制御手段とを有することを特徴とする。 The water treatment device according to claim 7 is a membrane fouling substance treatment means into which water to be treated containing a membrane fouling substance is introduced, and the water treated by the membrane fouling substance treatment means is subjected to membrane separation treatment and concentrated water. Separation device for separating water into permeated water, membrane fouling substance concentration measuring means for measuring the concentration of membrane fouling substance contained in the concentrated water from the membrane separation device, and membrane fouling substance concentration measuring means And a control means for controlling the membrane fouling substance processing means based on the measurement result of (2).
請求項8の水処理装置は、請求項7において、前記膜ファウリング物質処理手段は、酸化分解装置、凝集処理装置及び活性炭吸着装置よりなる群から選択される少なくとも1つであることを特徴とする。 The water treatment apparatus according to claim 8 is characterized in that, in claim 7, the membrane fouling substance treatment means is at least one selected from the group consisting of an oxidative decomposition apparatus, a coagulation treatment apparatus, and an activated carbon adsorption apparatus. To do.
本発明の膜分離装置被処理水の評価方法によれば、濃縮水中の膜ファウリング物質の測定結果に基づいて該被処理水の水質を評価するため、被処理水に含まれる微量の膜ファウリング物質を検知することができる。 According to the method for evaluating the water to be treated of the membrane separation apparatus of the present invention, since the quality of the water to be treated is evaluated based on the measurement result of the membrane fouling substance in the concentrated water, Ring material can be detected.
即ち、被処理水中の膜ファウリング物質が微量であっても、濃縮水にあっては膜ファウリング物質が濃縮される。このため、被処理水中の膜ファウリング物質の濃度が検出限界値未満であったとしても、濃縮水中の膜ファウリング物質濃度が検出限界値以上に濃縮されていれば、膜ファウリング物質を検知することができる。従って、この濃縮水中の膜ファウリング物質濃度の測定結果に基づいて、被処理水の水質評価を高精度で行うことができる。 That is, even if the amount of membrane fouling substance in the water to be treated is very small, the membrane fouling substance is concentrated in the concentrated water. For this reason, even if the concentration of the membrane fouling substance in the treated water is less than the detection limit value, the membrane fouling substance is detected if the concentration of the membrane fouling substance in the concentrated water is more than the detection limit value. can do. Therefore, based on the measurement result of the membrane fouling substance concentration in the concentrated water, the quality of the water to be treated can be evaluated with high accuracy.
本発明の膜分離装置被処理水の評価方法において、濃縮水の蛍光強度を測定することにより、濃縮水中の膜ファウリング物質の水質測定を行うことが好ましい。この場合、被処理水の水質評価を短時間で簡易にかつ的確に評価することができる。 In the method for evaluating the water to be treated of the membrane separation apparatus of the present invention, it is preferable to measure the water quality of the membrane fouling substance in the concentrated water by measuring the fluorescence intensity of the concentrated water. In this case, the quality of the water to be treated can be evaluated easily and accurately in a short time.
本発明の膜分離装置被処理水の評価方法は、膜ファウリング物質が、微量でも膜にファウリングを生じさせる非イオン界面活性剤である場合に、好適に適用される。 The method for evaluating the water to be treated of the membrane separation apparatus of the present invention is suitably applied when the membrane fouling substance is a nonionic surfactant that causes fouling in the membrane even in a small amount.
非イオン界面活性剤がアルキルフェニルエーテル型非イオン界面活性剤である場合、波長300〜370nmの範囲に蛍光強度ピークを有するため、波長300〜400nmの範囲の蛍光強度を測定することが好ましい。 When the nonionic surfactant is an alkylphenyl ether type nonionic surfactant, since it has a fluorescence intensity peak in the wavelength range of 300 to 370 nm, it is preferable to measure the fluorescence intensity in the wavelength range of 300 to 400 nm.
本発明の水処理方法及び水処理装置によれば、膜分離装置からの濃縮水中に含有される膜ファウリング物質の測定結果に基づき、膜ファウリング物質処理手段を制御するため、被処理水中の膜ファウリング物質を効率よく処理することができる。その結果、膜分離装置において高透過流束を維持することができ、長期にわたり安定した運転を継続することができる。 According to the water treatment method and the water treatment apparatus of the present invention, in order to control the membrane fouling substance treatment means based on the measurement result of the membrane fouling substance contained in the concentrated water from the membrane separator, The membrane fouling material can be processed efficiently. As a result, a high permeation flux can be maintained in the membrane separation apparatus, and a stable operation can be continued for a long time.
上記膜ファウリング物質処理手段としては、酸化分解装置、凝集処理装置及び活性炭吸着装置よりなる群から選択される少なくとも1つが好適である。 The membrane fouling substance treatment means is preferably at least one selected from the group consisting of an oxidative decomposition apparatus, a coagulation treatment apparatus, and an activated carbon adsorption apparatus.
以下に図面を参照して、本発明の膜分離装置被処理水の評価方法を採用した水処理方法及び水処理装置の実施の形態を詳細に説明する。 Embodiments of a water treatment method and a water treatment apparatus that employ a method for evaluating water to be treated of a membrane separation apparatus of the present invention will be described in detail below with reference to the drawings.
第1図は本発明の水処理装置の実施の形態を示す系統図である。 FIG. 1 is a system diagram showing an embodiment of the water treatment apparatus of the present invention.
第1図の水処理装置は、膜ファウリング物質を含む被処理水を、膜ファウリング物質処理装置1及び膜分離装置2で順次処理して透過水とすると共に、該膜分離装置2からの濃縮水に含まれる膜ファウリング物質を膜ファウリング物質濃度測定装置3で測定し、この測定結果に基づいて前記膜ファウリング物質処理装置1を制御器4で制御するものである。 The water treatment apparatus of FIG. 1 sequentially treats water to be treated containing a membrane fouling substance with a membrane fouling substance treatment apparatus 1 and a membrane separation apparatus 2 to obtain permeated water. The membrane fouling substance contained in the concentrated water is measured by the membrane fouling substance concentration measuring device 3, and the membrane fouling substance treatment device 1 is controlled by the controller 4 based on the measurement result.
なお、膜分離装置2からの透過水は、必要に応じてさらに処理された後、純水あるいは超純水として使用される。また、膜分離装置2からの濃縮水は、必要に応じて前記膜ファウリング物質除去装置1の洗浄水や、冷却水補給水などとして使用される。 The permeated water from the membrane separation device 2 is further processed as necessary, and then used as pure water or ultrapure water. Further, the concentrated water from the membrane separation device 2 is used as washing water, cooling water replenishing water, or the like of the membrane fouling substance removing device 1 as necessary.
膜ファウリング物質処理装置1としては、オゾン酸化装置、紫外線酸化装置、紫外線併用オゾン促進酸化装置などの酸化分解装置、凝集濾過器などの凝集処理装置、活性炭吸着装置及びイオン交換装置の少なくとも1つ又はこれらを組み合わせたものが好適である。 The membrane fouling substance treatment apparatus 1 includes at least one of an oxidative decomposition apparatus such as an ozone oxidizer, an ultraviolet oxidizer, and an ozone accelerated oxidizer combined with ultraviolet rays, an flocculation treatment apparatus such as a flocculation filter, an activated carbon adsorption apparatus, and an ion exchange apparatus Or a combination of these is preferred.
オゾン酸化装置、オゾン促進酸化装置、紫外線酸化装置などの酸化分解装置では、オゾンや紫外線により有機物質を有機酸、さらにはCO2まで分解する。凝集処理装置では、被処理水中の懸濁物質やコロイド物質等の除去を行う。活性炭吸着装置では、有機物質、残留塩素、微粒子等を活性炭に吸着させて除去する。 In an oxidative decomposition apparatus such as an ozone oxidizer, an ozone accelerating oxidizer, or an ultraviolet oxidizer, an organic substance is decomposed into an organic acid and further to CO 2 by ozone or ultraviolet rays. The aggregating apparatus removes suspended substances, colloidal substances and the like in the water to be treated. In the activated carbon adsorption device, organic substances, residual chlorine, fine particles, and the like are adsorbed and removed by activated carbon.
膜分離装置2に用いられる分離膜の材質に特に制限はなく、例えばポリアミド系分離膜、セルロースエステル系分離膜、ポリスルホン系分離膜、ポリイミド系分離膜などを挙げることができる。 There is no restriction | limiting in particular in the material of the separation membrane used for the membrane separation apparatus 2, For example, a polyamide-type separation membrane, a cellulose-ester-type separation membrane, a polysulfone-type separation membrane, a polyimide-type separation membrane etc. can be mentioned.
また、膜分離装置2の膜モジュールの種類にも特に制限はなく、例えばスパイラルモジュール、中空糸モジュール、平面膜モジュール、管型モジュールなどを用いることができる。 Moreover, there is no restriction | limiting in particular also in the kind of membrane module of the membrane separation apparatus 2, For example, a spiral module, a hollow fiber module, a plane membrane module, a tubular module etc. can be used.
この膜分離装置2では、塩類を除去すると共に、イオン性、コロイド性の有機物質を除去する。 In the membrane separation device 2, salts are removed and ionic and colloidal organic substances are removed.
膜ファウリング物質濃度測定装置3としても特に制限はなく、蛍光強度測定装置、吸光光度測定装置、比抵抗測定装置、有機物質(TOC)濃度測定装置等が用いられるが、特に蛍光強度測定装置が好適に用いられる。 The membrane fouling substance concentration measurement device 3 is not particularly limited, and a fluorescence intensity measurement device, an absorptiometry device, a specific resistance measurement device, an organic substance (TOC) concentration measurement device, and the like are used. Preferably used.
蛍光強度測定装置は、紫外線吸光度を測定する吸光光度測定装置に比べて1桁から2桁は感度が高いため、高精度の分析を行うことができる。例えば、被処理水にアルキルフェニルエーテル型非イオン界面活性剤が含まれる場合、フェニル基は紫外線吸収波長及び紫外線励起−蛍光波長を有するため、吸光光度測定装置及び蛍光強度測定装置の両方を用いることができるが、より感度の高い蛍光強度測定装置を用いることが好ましい。 Since the fluorescence intensity measuring device is 1 to 2 digits more sensitive than the absorptiometric device that measures ultraviolet absorbance, it is possible to perform highly accurate analysis. For example, when the water to be treated contains an alkylphenyl ether type nonionic surfactant, the phenyl group has an ultraviolet absorption wavelength and an ultraviolet excitation-fluorescence wavelength, so use both an absorptiometry device and a fluorescence intensity measurement device. However, it is preferable to use a fluorescence intensity measuring device with higher sensitivity.
なお、被処理水に非イオン界面活性剤が含まれている場合は、その濃度が微量でも、膜を著しくファウリングさせる。本発明者は、市販の蛍光分析計でアルキルフェニルエーテル型非イオン界面活性剤を分析した結果、蛍光波長300〜400nmの範囲に、1つ又は複数の蛍光を発光することを見出した。この範囲、好ましくは300〜370nm、特に300〜350nmの範囲の波長での蛍光強度とアルキルフェニルエーテル型非イオン界面活性剤の濃度との間に一次の相関があり、この範囲内の蛍光強度をアルキルフェニルエーテル型非イオン界面活性剤の濃度に換算することができることも認められた。従って、被処理水中にアルキルフェニルエーテル型非イオン界面活性剤が含まれる場合、波長300〜400nm、好ましくは300〜370nm、特に300〜350nmの範囲の波長での蛍光強度を測定することが好ましい。 In addition, when a nonionic surfactant is contained in to-be-processed water, even if the density | concentration is a trace amount, a film | membrane is remarkably fouled. As a result of analyzing an alkylphenyl ether type nonionic surfactant with a commercially available fluorescence analyzer, the present inventor has found that one or a plurality of fluorescences are emitted in a fluorescence wavelength range of 300 to 400 nm. There is a first-order correlation between the fluorescence intensity at a wavelength in this range, preferably 300 to 370 nm, particularly 300 to 350 nm, and the concentration of the alkylphenyl ether type nonionic surfactant. It was also recognized that it could be converted to the concentration of alkyl phenyl ether type nonionic surfactant. Therefore, when the alkylphenyl ether type nonionic surfactant is contained in the water to be treated, it is preferable to measure the fluorescence intensity at a wavelength in the range of 300 to 400 nm, preferably 300 to 370 nm, particularly 300 to 350 nm.
上記蛍光強度測定装置としては、通常の蛍光分析計を用いることができる。また、励起光の波長、蛍光の波長及び蛍光強度からなる三次元蛍光スペクトルを得る装置を用いてもよく、この場合、蛍光波長の異なる複数種の膜汚染物質(膜ファウリング物質)を同時に測定することができる。 As the fluorescence intensity measuring device, a normal fluorescence analyzer can be used. In addition, a device that obtains a three-dimensional fluorescence spectrum consisting of the wavelength of excitation light, the wavelength of fluorescence, and the intensity of fluorescence may be used. In this case, multiple types of membrane contaminants (membrane fouling materials) having different fluorescence wavelengths can be measured simultaneously. can do.
制御器4は、上記膜ファウリング物質濃度測定装置3による濃縮水中の膜ファウリング物質濃度の測定結果を受信し、この測定結果に基づいて被処理水中の膜ファウリング物質濃度を評価し、この評価結果に基づいて、上記膜ファウリング物質処理装置1を制御するものである。 The controller 4 receives the measurement result of the membrane fouling substance concentration in the concentrated water by the membrane fouling substance concentration measuring device 3 and evaluates the membrane fouling substance concentration in the treated water based on the measurement result. The membrane fouling substance processing apparatus 1 is controlled based on the evaluation result.
膜ファウリング物質処理装置1の制御方法には特に制限はない。例えば、膜ファウリング物質処理装置1がオゾン酸化装置である場合、オゾン発生電流を変化させ、オゾン発生量を制御する。膜ファウリング物質処理装置1が凝集処理装置である場合、凝集剤注入量を制御する。膜ファウリング物質処理装置1が活性炭吸着装置である場合、濃縮水中の膜ファウリング物質濃度の測定結果に基づいて、活性炭の吸着力が飽和に達したか否かを判定する。飽和に達したと判定すると、制御器がメインの活性炭吸着装置から予備の活性炭吸着装置に被処理水の通水を切替える。この切替運転の間に、メインの活性炭吸着装置内における活性炭の交換を行う。膜ファウリング物質処理装置1がイオン交換装置である場合、濃縮水中の膜ファウリング物質濃度の測定結果に基づいて、イオン交換装置内に充填されたイオン交換樹脂の再生や、予備のイオン交換装置への通水切替等を行う。 There is no restriction | limiting in particular in the control method of the membrane fouling substance processing apparatus 1. FIG. For example, when the membrane fouling material processing apparatus 1 is an ozone oxidizer, the ozone generation current is changed to control the ozone generation amount. When the membrane fouling substance processing apparatus 1 is an aggregating apparatus, the amount of flocculant injected is controlled. When the membrane fouling substance processing apparatus 1 is an activated carbon adsorption apparatus, it is determined whether or not the adsorption power of activated carbon has reached saturation based on the measurement result of the membrane fouling substance concentration in the concentrated water. When it is determined that the saturation has been reached, the controller switches the flow of the water to be treated from the main activated carbon adsorption device to the spare activated carbon adsorption device. During this switching operation, the activated carbon is exchanged in the main activated carbon adsorption device. When the membrane fouling material treatment device 1 is an ion exchange device, based on the measurement result of the membrane fouling material concentration in the concentrated water, regeneration of the ion exchange resin filled in the ion exchange device or a spare ion exchange device Switch the water flow to and from.
第2図は、本発明の水処理装置の異なる実施の形態を示す系統図である。 FIG. 2 is a system diagram showing a different embodiment of the water treatment apparatus of the present invention.
第2図の水処理装置は、膜ファウリング物質を含む被処理水(低濃度排水)を、オゾン酸化槽11、活性炭塔12、凝集濾過器13、イオン交換塔14及び逆浸透膜(RO膜)装置15で順次水処理して透過水とし、さらにこの透過水をサブシステム16で水処理して超純水とするものである。
The water treatment apparatus of FIG. 2 is configured to treat water (low-concentration wastewater) containing a membrane fouling substance into an
この水処理装置では、活性炭塔12で処理した水に工水および凝集剤を添加混合し、この混合水を凝集濾過器13に導入している。
In this water treatment apparatus, industrial water and a flocculant are added and mixed with the water treated by the activated
この水処理装置は、逆浸透膜装置15からの濃縮水中の膜ファウリング物質を測定する蛍光分析計17を備えている。この蛍光分析計17は、オゾン酸化槽11のオゾン発生電流を制御する制御器を備えている。逆浸透膜装置15からの濃縮水の一部は蛍光分析計17に供給され、濃縮水に含まれる膜ファウリング物質の濃度がこの蛍光分析計17で測定される。この測定結果に基づき、この蛍光分析計17内の制御器がオゾン酸化槽11のオゾン発生電流を制御する。なお、この濃縮水は、再生用水等として使用される。
This water treatment device includes a
オゾン酸化槽11では、被処理水中の有機物質を、オゾンによって有機酸、さらにはCO2まで分解する。
In the
活性炭塔12では、有機物質、残留オゾン、微粒子等を活性炭に吸着させて除去する。
In the activated
凝集濾過器13では、凝集フロックを濾材で濾過する。即ち、凝集濾過器13の上流側において、被処理水中に、硫酸バンド、ポリ塩化アルミニウム(PAC)などの凝集剤と工水とを添加し、アルミニウム塩などのフロックを形成させる。この凝集フロックを、濾材のスクリーン作用及び吸着作用で濾過する。
In the
なお、この工水は、この水処理装置で製造した超純水を循環再使用する場合に、濃縮水としてこの循環系外に排出された分だけの水を補給するためのものである。 In addition, this industrial water is for replenishing only the part discharged | emitted out of this circulation system as concentrated water when the ultrapure water manufactured with this water treatment apparatus is circulated and reused.
イオン交換塔14では、塩類を除去すると共に、イオン交換樹脂によって吸着又はイオン交換される有機物質の除去を行う。
In the
逆浸透膜装置15では、塩類を除去すると共に、上流側では除去しきれなかったイオン性、コロイド性の有機物質を除去する。
The reverse
サブシステム16は、例えば、逆浸透膜装置15からの透過水を、サブタンク、熱交換器、低圧紫外線酸化装置、イオン交換塔及び限外濾過膜分離装置で順次水処理するものである。このサブシステム16で処理された超純水は、ユースポイントに供給される。
For example, the sub-system 16 sequentially treats the permeated water from the reverse
本実施の形態によると、逆浸透膜装置からの透過水の流束を維持することができ、長期にわたり安定した運転を継続することができる。また、オゾン酸化槽11で発生させるオゾン量を適量に制御することができるため、透過水の水質を維持すると共に、無駄なエネルギー消費を防止することができる。
According to this embodiment, the flux of permeated water from the reverse osmosis membrane device can be maintained, and stable operation can be continued for a long time. Moreover, since the amount of ozone generated in the
上記実施の形態は本発明の一例であり、本発明は上記実施の形態に限定されるものではない。例えば、第2図の水処理装置では、蛍光分析計17内の制御器によってオゾン酸化槽11を制御しているが、オゾン酸化槽11の制御に代えて、又はオゾン酸化槽11の制御に加えて、活性炭塔12、凝集濾過器13及びイオン交換塔14の少なくとも1つを制御するようにしてもよい。
The above embodiment is an example of the present invention, and the present invention is not limited to the above embodiment. For example, in the water treatment apparatus of FIG. 2, the
また、第3図に示す通り、イオン交換塔14の設置位置を逆浸透膜装置15の後段側かつサブシステム16の上流側としてもよい。
Further, as shown in FIG. 3, the
以下に、実施例1を挙げて本発明をより具体的に説明するが、本発明はその要旨を超えない限り、以下の実施例1により何ら限定されるものではない。 Hereinafter, the present invention will be described more specifically with reference to Example 1. However, the present invention is not limited to the following Example 1 as long as the gist thereof is not exceeded.
実施例1
<第1の運転例>
第2図の水処理装置のうちサブシステム16を省略したものを用いて、被処理水の水処理を行った。
Example 1
<First operation example>
The water to be treated was treated using the water treatment apparatus of FIG. 2 without the
なお、被処理水として、液晶製造工程で排出される水洗水(TOC濃度:5.5mg/L、アルキルフェニルエーテル型非イオン界面活性剤(APE)濃度:2.2mg/L as TOC)を用いた。 In addition, washing water discharged in the liquid crystal manufacturing process (TOC concentration: 5.5 mg / L, alkylphenyl ether type nonionic surfactant (APE) concentration: 2.2 mg / L as TOC) is used as the water to be treated. It was.
蛍光分析計17として、日立ハイテク社製FL4500型を用いた。また、後述する通り、逆浸透膜装置15からの濃縮水に加えて、逆浸透膜装置15の入口水の測定も同機種の蛍光分析計を用いて行った。
As the
先ず、この被処理水に対して過酸化水素10mg/Lを添加した後、この被処理水を水酸化ナトリウムでpH10.5になるように調整した。 First, after adding 10 mg / L of hydrogen peroxide to the water to be treated, the water to be treated was adjusted to pH 10.5 with sodium hydroxide.
この被処理水をオゾン酸化槽11に導入してオゾンガスを吹き込み、この被処理水中に40mg/Lのオゾンガスを溶解させたオゾン処理水を得た。このオゾン処理水の水質を測定した結果、pH9.8、電気伝導率15mS/m、TOC濃度2.1mg/L、APE濃度0.1mg/L as TOC以下、残存オゾン濃度0.5mg/L以下であった。
This treated water was introduced into the
なお、このAPE濃度は、ポリエキシエチレンオクチルフェニルエーテル(日本油脂株式会社製、商品名「ノニオンHS−210」)を標準物質とし、励起波長230nm、蛍光波長315nmの蛍光強度で作成した検量線より求めた。なお、定量下限値は0.1mg/L as TOCであった。 This APE concentration is obtained from a calibration curve prepared with fluorescence intensity at an excitation wavelength of 230 nm and a fluorescence wavelength of 315 nm using polyoxyethylene octylphenyl ether (Nippon Yushi Co., Ltd., trade name “Nonion HS-210”) as a standard substance. Asked. The lower limit of quantification was 0.1 mg / L as TOC.
このオゾン処理水を、活性炭塔12(空塔速度10L/h)、凝集濾過器13(PAC添加量10mg/L、凝集pH6.5)、混床式のイオン交換塔14(空塔速度30L/h)の順で処理してイオン交換処理水を得た。その結果、このイオン交換処理水は、比抵抗10MΩ/cm、TOC濃度140μg/L、APE濃度0.1mg/L as TOC以下であった。 This ozone-treated water was mixed with activated carbon tower 12 (superficial speed 10 L / h), coagulation filter 13 (PAC addition amount 10 mg / L, coagulation pH 6.5), mixed bed ion exchange tower 14 (superficial speed 30 L / h). It processed in the order of h), and obtained the ion exchange treated water. As a result, this ion exchange treated water had a specific resistance of 10 MΩ / cm, a TOC concentration of 140 μg / L, and an APE concentration of 0.1 mg / L as TOC or less.
このイオン交換処理水を、逆浸透膜装置15(逆浸透平膜:日東電工社製ES20フラットシート、Φ75mm、超純水洗浄品)に、運転圧力0.74MPa、透過水量125mL/h、回収率90%の条件で連続通水して透過水を得た。その結果、運転圧力及び透過水量を変化させることなく80時間の連続運転を行うことができた。透過水中のTOC濃度は50μg/Lであった。また、逆浸透膜装置15の入口水及び濃縮水の蛍光強度を蛍光分析計を用いて測定した結果、いずれも検出下限値以下であった。
This ion exchange treated water was applied to a reverse osmosis membrane device 15 (reverse osmosis flat membrane: ES20 flat sheet manufactured by Nitto Denko Corporation, Φ75 mm, ultrapure water washed product) at an operating pressure of 0.74 MPa, a permeated water amount of 125 mL / h, and a recovery rate. Permeated water was obtained by continuously passing water under the condition of 90%. As a result, continuous operation for 80 hours could be performed without changing the operating pressure and the amount of permeated water. The TOC concentration in the permeated water was 50 μg / L. Moreover, as a result of measuring the fluorescence intensity of the inlet water and concentrated water of the reverse
<第2の運転例>
オゾン酸化槽11において被処理水にオゾンを吹き込む量を減少させ、被処理水中に30mg/Lのオゾンガスを溶解させたこと以外は、第1の運転例と同じ条件で透過水を得た。
<Second operation example>
Permeated water was obtained under the same conditions as in the first operation example, except that the amount of ozone blown into the water to be treated in the
その結果、運転開始から60分後において、オゾン処理水は、pH9.8、電気伝導率15mS/m、TOC濃度2.4mg/L、APE濃度0.1mg/L as TOC以下、残存オゾン濃度0.5mg/L以下であった。また、イオン交換処理水は、比抵抗10MΩ/cm、TOC濃度170μg/L、APE濃度0.1mg/L as TOC以下であった。 As a result, after 60 minutes from the start of operation, the ozone-treated water had a pH of 9.8, an electrical conductivity of 15 mS / m, a TOC concentration of 2.4 mg / L, an APE concentration of 0.1 mg / L as TOC or less, and a residual ozone concentration of 0. 0.5 mg / L or less. The ion-exchanged water had a specific resistance of 10 MΩ / cm, a TOC concentration of 170 μg / L, and an APE concentration of 0.1 mg / L as TOC or less.
しかしながら、運転を続けるに従い、透過水量が徐々に低下し、60時間後における透過水量は106mL/hに低下した。また、透過水中のTOC濃度は45μg/Lであった。なお、逆浸透膜装置15の入口水の蛍光分析計17による蛍光強度は検出下限値以下であったが、濃縮水中のAPE濃度は0.2mg/Lであった。
However, as the operation continued, the amount of permeated water gradually decreased, and the amount of permeated water after 60 hours decreased to 106 mL / h. Further, the TOC concentration in the permeated water was 45 μg / L. In addition, although the fluorescence intensity by the
<第3の運転例>
第2の運転例の直後に、運転条件を第1の運転例に戻した。
<Third operation example>
Immediately after the second operation example, the operating conditions were returned to the first operation example.
その結果、逆浸透膜装置15からの透過水の水量は徐々に増加し、200時間後に120mL/hに回復した。また、第3の運転例における濃縮水の蛍光強度は38以下であり、APE検出下限値以下であった。
As a result, the amount of permeated water from the reverse
1 膜ファウリング物質処理装置
2 膜分離装置
3 膜ファウリング物質濃度測定装置
4 制御器
11 オゾン酸化槽
12 活性炭槽
13 凝集濾過器
14 イオン交換塔
15 逆浸透膜装置
16 サブシステム
17 蛍光分析計
DESCRIPTION OF SYMBOLS 1 Membrane fouling substance processing apparatus 2 Membrane separation apparatus 3 Membrane fouling substance concentration measurement apparatus 4
Claims (8)
該膜分離装置からの濃縮水中の膜ファウリング物質濃度を測定し、この測定結果に基づいて該被処理水の水質を評価することを特徴とする膜分離装置被処理水の評価方法。 A method for evaluating the quality of water to be treated containing a membrane fouling substance supplied to a membrane separator,
A method for evaluating water to be treated in a membrane separator, comprising measuring a membrane fouling substance concentration in concentrated water from the membrane separator and evaluating the quality of the water to be treated based on the measurement result.
該膜分離装置からの濃縮水中に含有される膜ファウリング物質濃度を測定し、この測定結果に基づき、前記膜ファウリング物質処理手段を制御することを特徴とする水処理方法。 In a water treatment method in which water to be treated containing a membrane fouling substance is treated with a membrane fouling substance treatment means and then separated into concentrated water and permeated water by membrane separation treatment with a membrane separation device.
A water treatment method characterized by measuring a membrane fouling substance concentration contained in concentrated water from the membrane separator and controlling the membrane fouling substance treatment means based on the measurement result.
該膜ファウリング物質処理手段で処理された水を膜分離処理して濃縮水と透過水とに分離する膜分離装置と、
該膜分離装置からの濃縮水中に含有される膜ファウリング物質の濃度を測定する膜ファウリング物質濃度測定手段と、
この膜ファウリング物質濃度測定手段の測定結果に基づき、前記膜ファウリング物質処理手段を制御する制御手段と
を有することを特徴とする水処理装置。 A membrane fouling substance treatment means into which treated water containing a membrane fouling substance is introduced;
A membrane separation device for separating the water treated by the membrane fouling substance treatment means into a concentrated water and a permeated water by a membrane separation treatment;
Membrane fouling substance concentration measuring means for measuring the concentration of the membrane fouling substance contained in the concentrated water from the membrane separation device;
A water treatment apparatus comprising: control means for controlling the membrane fouling substance treatment means based on the measurement result of the membrane fouling substance concentration measurement means.
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Cited By (13)
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JP2010195750A (en) * | 2009-02-27 | 2010-09-09 | Osaka Municipal Technical Research Institute | Amphiphilic substance, surfactant, and method of using surfactant |
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JP2010195750A (en) * | 2009-02-27 | 2010-09-09 | Osaka Municipal Technical Research Institute | Amphiphilic substance, surfactant, and method of using surfactant |
JP2011083666A (en) * | 2009-10-13 | 2011-04-28 | Miura Co Ltd | Water treatment system |
WO2012124538A1 (en) * | 2011-03-15 | 2012-09-20 | 株式会社 東芝 | Fouling prediction method, and membrane filtration system |
JP2012192315A (en) * | 2011-03-15 | 2012-10-11 | Toshiba Corp | Fouling prediction method, and membrane filtration system |
JP2013193075A (en) * | 2012-03-23 | 2013-09-30 | Hitachi Ltd | Desalination system |
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JP2018012062A (en) * | 2016-07-21 | 2018-01-25 | 水ing株式会社 | Membrane blockage estimation method and membrane blockage estimation device of reverse osmosis membrane supply water, and operation management method of water treatment equipment using the membrane blockage estimation method |
JP2018179556A (en) * | 2017-04-04 | 2018-11-15 | 三浦工業株式会社 | Water quality monitoring device and water treatment system |
WO2019225306A1 (en) * | 2018-05-21 | 2019-11-28 | 栗田工業株式会社 | Reverse osmosis system diagnostic device |
JP2019202305A (en) * | 2018-05-21 | 2019-11-28 | 栗田工業株式会社 | Diagnosis device of reverse osmosis system |
JP2019202243A (en) * | 2018-05-21 | 2019-11-28 | 栗田工業株式会社 | Diagnosis device of reverse osmosis system |
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