JP4151946B2 - Method for reforming membrane treated water - Google Patents
Method for reforming membrane treated water Download PDFInfo
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- JP4151946B2 JP4151946B2 JP2002307979A JP2002307979A JP4151946B2 JP 4151946 B2 JP4151946 B2 JP 4151946B2 JP 2002307979 A JP2002307979 A JP 2002307979A JP 2002307979 A JP2002307979 A JP 2002307979A JP 4151946 B2 JP4151946 B2 JP 4151946B2
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- membrane
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Description
【0001】
【発明の属する技術分野】
本発明は、膜ろ過装置の処理水の改質方法に関するもので、特にろ過水を上水や工業用水や修景用水などに利用するための改質方法に関する。
【0002】
【従来の技術】
従来、上下水道、医薬品、食品など多くの施設で用いられる浄水を得る方法として膜ろ過法が広く利用されている。膜ろ過法は、ろ過膜により原水中の懸濁物質を除去する固液分離の技術であり、ろ過の進行に伴い、1次側のろ過膜面に原水中の懸濁物質が積層してケーキ層を形成する。このケーキ層によってろ過抵抗が徐々に増大し、ろ過性能が低下するようになる。
【0003】
そこで、通常の膜ろ過法では、ケーキ層がある程度厚くなった時点で逆洗浄を行い、ろ過性能を回復させている。この逆洗浄(以下、単に逆洗という)は、図2において、ろ過膜1の2次側(ろ過水側)12から1次側(原水側)11に向けて洗浄水を通水させ、ろ過膜1面上のケーキ層を剥離、除去するようにした膜の洗浄法である。
【0004】
【特許文献1】
特開平7−60072号公報
【特許文献2】
特開平7−124448号公報
また、この膜ろ過装置のろ過膜1の表面には微生物が繁殖し易く、この繁殖した微生物がろ過抵抗を特に増大させる原因ともなっている。そこで、この微生物の繁殖を防止するために、原水槽13中や原水配管に酸化剤供給タンク14から殺菌用の酸化剤を添加しながらろ過運転を行ったり、また上記の特許文献1、2に記載されているように、前記逆洗時には、2次側12から供給される逆洗水に酸化剤供給タンク15から次亜塩素酸など酸化剤を添加して殺菌することが、通常行われている。なお酸化剤には、次亜塩素酸や二酸化塩素などの塩素成分を含む薬剤、過酸化水素、オゾンなどを用いている。また、オゾンなどを使用する場合には、酸化剤供給タンク14を使用せず、直接水に溶解させることもある。
【0005】
ところが、このような膜ろ過装置から得られる処理水には、原水中に含まれるマンガン、鉄などの微量のイオン状金属成分が析出して、微小析出物として混在するため、水質が低下することが分ってきた。特に、このような金属成分の微小析出物は、ろ過水を上水や工業用水や修景用水などに利用する場合には好ましくなかった。また、このような処理水を後段のUF膜、NF膜、RO膜などで高度膜ろ過処理を行う場合には、前記微小析出物がろ過膜を閉塞する原因となるなど、解決課題の一つであった。
【0006】
【発明が解決しようとする課題】
本発明は、上記の問題点を解決するためになされたものであり、膜ろ過装置の運転において、原水中に含まれるマンガン、鉄などの微量のイオン状金属成分が、処理水中に微小析出物として析出するのを防止する膜処理水の改質方法を提供する。
【0007】
【課題を解決するための手段】
本件発明者らは、原水中に含まれるマンガン、鉄などの微量のイオン状金属成分の析出現象と添加される微生物殺菌用の酸化剤との関係を調査研究した結果、酸化剤の存在がイオン状金属成分の微小析出物への変化を促進するという事実を見出したことにより、本発明を完成させるに到ったのである。
【0008】
そして、上記問題を解決することができる膜処理水の改質方法は、マンガン、鉄のイオン状金属成分を含有する原水を対象とした膜ろ過装置のろ過運転および逆洗操作時において、原水中の前記金属成分がろ過後に微小析出物として2次側の処理水中に析出しないよう、ろ過運転時には、原水に酸化剤を添加することなくろ過運転し、逆洗時には、1次側に酸化剤を添加した洗浄水を送給して1次側を洗浄し、次いで酸化剤を添加しない逆洗水をろ過膜の2次側から送給して、ケーキ層を剥離させ、1次側に残留する酸化剤とともに除去することを特徴とするものである。
また、本発明の膜処理水の改質方法は、さらに、前記膜ろ過装置から得た処理水を、後段のUF膜、NF膜、RO膜による高度膜ろ過処理を行う形態に具体化される。
【0009】
【発明の実施の形態】
次に、本発明の膜処理水の改質方法に係る実施形態について、図1を参照しながら説明する。
図1は、本発明の膜処理水の改質方法が適用できる膜ろ過装置の模式的フローを例示するものであり、本発明では、▲1▼ろ過運転、▲2▼逆洗操作のそれぞれをつぎに説明する条件で運転する点に特徴がある。
【0010】
1.ろ過運転:マンガン、鉄などの微量のイオン状金属成分を含む原水に、次亜塩素酸などの酸化剤を添加することなく、ろ過運転を行う。すなわち、原水は原水槽21から膜ろ過装置3の1次側31に送り込まれ、ろ過されるとともに、残部は原水槽21にリターンするよう循環送給されるが、この原水には、従来添加される酸化剤は全く使用しないのである。なお、洗浄水槽22への逆洗水の供給は、通常ろ過水の一部を用いて行える。
【0011】
▲2▼逆洗操作:ろ過運転を中止または中止直前に、酸化剤供給タンク22に入っている次亜塩素酸や二酸化塩素などの塩素成分を含む薬剤、過酸化水素などの酸化剤を添加した1次洗浄水をろ過膜30の1次側31に送給して、1次側31内と積層したケーキ層を洗浄し、殺菌する。次いで、2次側32に洗浄水槽23から逆洗水を送給して、ろ過膜30の逆洗を行うのであるが、この逆洗水には、従来のように酸化剤を添加することはしない。かくして、1次側31内の殺菌、洗浄と、積層したケーキ層の剥離、除去が行われるとともに、1次洗浄水によって持ち込まれた酸化剤は系外に除去されるのである。なお、用済みの洗浄水は、排出バルブ31aを経て排出される。また、一次洗浄水には、原水やろ過水を、酸化剤を調整して用いることができる。さらに、酸化剤としてオゾンなどを用いる場合は、酸化剤供給タンク22を使用せずに原水に直接注入することもできる。
【0012】
以上説明したように、本発明における膜ろ過装置の運転方法によれば、膜ろ過装置に送給された酸化剤は用済みの洗浄水とともに排出するようにしているから、酸化剤と反応した原水中の化学成分が2次側32に流出することがなくなるので、前記したような微小な金属析出物の2次側の処理水中への析出に基づく障害も完全に解消できるのである。
【0013】
そして、さらに図1の例示のように、本発明の前記した膜ろ過装置3を前段に位置づけ、後段にUF膜(限外ろ過膜)、NF膜(ナノろ過膜)、RO膜(逆浸透膜)などの高度膜ろ過装置4を配置して高度膜処理を行い、高純度の処理水を製造するシステムを構築すれば、前段の膜ろ過装置3から得た処理水によって、後段のUF膜、NF膜、RO膜などの高度ろ過膜に微小な金属析出物に起因する閉塞などの不具合が発生しないので、システム全体が効果的に運転できる利点が得られるのである。
【0014】
ここで、本発明の効果を下記条件で実測した結果を表1に例示する。
表1の結果によれば、従来の運転条件のように、原水に酸化剤を添加する比較例1、2の処理水のFI値は、逆洗水の酸化剤の添加を1次、2次を入れ換えて見ても、高い値を示している。また、原水への塩素添加を省略する比較例3のケースでも、本発明のような低いFI値は得られていない。
【0015】
なお、実施例と比較例の試験条件は、次の通りである。
使用原水は、下水の二次処理水(最終沈殿池の上澄み水)を使用した。
ろ過工程では、原水にPAC(ポリ塩化アルミニウム)を加え凝集した後に、セラミック製のMF膜によりデッドエンド方式で膜ろ過を行った。膜の洗浄は、まず酸化剤供給タンク22から酸化剤として次亜塩素を塩素成分濃度が50ppmとなるように調整した1次洗浄水をろ過膜30の1次側31に送給して、1次側31内と積層したケーキ層を洗浄し、殺菌した。次いで、2次側32に酸化剤を添加していない逆洗水を送給して、ろ過膜30の逆洗を行った。
比較実験では、上記原水を上記方法で膜ろ過を行い、膜洗浄のみ変更した。つまり膜洗浄の際に各々一次洗浄水と逆洗水に次亜塩素水を添加した水、無添加の水を用いた。
【0016】
なお、FI値(ファウリングインデックス)は、所定の処理水量を得るのに要する時間を表示するもので、次式で表される。
FI = (1−T0 / T15)×100 / 15
ここでT0は、0.45μmの精密ろ過膜を用いて、試料水を206kPaの加圧下でろ過するときに、初めに500mlをろ過するのに要した時間である。またT15は、T0と同じ状態で15分間継続してろ過した後に、500mlをろ過するのに要した時間である。FI値は、小さいほど良い(微粒子含有量が少ない)ことになる。
【0017】
【表1】
【0018】
なお、本発明の膜処理水の改質方法は、高分子あるいはセラミックス材料からなるMF膜(精密ろ過膜)、UF膜(限外ろ過膜)などをモノリス、中空糸、チューブラ、ハニカムまたは平膜形状に構成し、加圧方式は外圧式、内圧式など、ろ過方式はクロスフローやデッドエンドなど多岐にわたる形式の膜ろ過装置に適用可能である。また、被処理水としては特に限定されない。例えば、下水、返流水、工場排水、ごみ浸出水、屎尿、農業廃水、畜産廃水、養殖排水などの排水・廃水処理はもちろんのこと、上水処理も対象とされ得る。
【0019】
【発明の効果】
本発明の膜処理水の改質方法は、以上説明したように構成されているので、原水中に含まれるマンガン、鉄などの微量のイオン状金属成分が、処理水中に微小析出物として析出するのを防止することが可能となり、高純度の処理水を提供することができる。また、後段にUF膜、NF膜、RO膜などの高度ろ過膜を併設でき、さらに高度な膜ろ過システムが構築できるという優れた効果がある。よって本発明は、従来の問題点を解消した膜処理水の改質方法として、その実用的価値はきわめて大なるものがある。
【図面の簡単な説明】
【図1】本発明の実施形態を説明するための膜ろ過装置の模式的フロー図。
【図2】従来の膜ろ過装置の要部を示す模式的フロー図。
【符号の説明】
21 原水槽、22 酸化剤供給タンク、23 洗浄水槽、3 膜ろ過装置、30 ろ過膜、31 1次側、31a 排出バルブ、32 2次側、4 高度膜ろ過装置。[0001]
BACKGROUND OF THE INVENTION
The present invention relates to a method for reforming treated water of a membrane filtration device, and more particularly to a method for reforming filtered water for use in tap water, industrial water, landscape water, or the like.
[0002]
[Prior art]
Conventionally, a membrane filtration method has been widely used as a method for obtaining purified water used in many facilities such as water and sewage systems, pharmaceuticals, and foods. The membrane filtration method is a solid-liquid separation technology that removes suspended solids in raw water using a filtration membrane. As the filtration progresses, suspended solids in the raw water are layered on the primary filtration membrane. Form a layer. This cake layer gradually increases the filtration resistance and lowers the filtration performance.
[0003]
Therefore, in the normal membrane filtration method, when the cake layer becomes thick to some extent, back washing is performed to restore the filtration performance. This backwashing (hereinafter simply referred to as backwashing) is performed by passing wash water from the secondary side (filtered water side) 12 of the
[0004]
[Patent Document 1]
Japanese Patent Laid-Open No. 7-60072 [Patent Document 2]
JP, 7-124448, A Moreover, microorganisms are easy to propagate on the surface of
[0005]
However, in the treated water obtained from such a membrane filtration device, trace amounts of ionic metal components such as manganese and iron contained in the raw water are precipitated and mixed as fine precipitates, so that the water quality deteriorates. I know. In particular, such metal component fine precipitates are not preferable when the filtered water is used for clean water, industrial water, landscape water, or the like. In addition, when such a treated water is subjected to advanced membrane filtration treatment in a subsequent UF membrane, NF membrane, RO membrane, etc., one of the problems to be solved is that the fine precipitates may block the filtration membrane. Met.
[0006]
[Problems to be solved by the invention]
The present invention has been made to solve the above problems, and in operation of the membrane filtration device, a minute amount of ionic metal components such as manganese and iron contained in the raw water are converted into fine precipitates in the treated water. The present invention provides a method for modifying membrane-treated water that prevents precipitation.
[0007]
[Means for Solving the Problems]
As a result of investigating the relationship between the precipitation phenomenon of trace amounts of ionic metal components such as manganese and iron contained in the raw water and the added oxidizing agent for sterilizing microorganisms, the present inventors found that the presence of the oxidizing agent is an ion. The present invention has been completed by finding the fact that the change of the metal-like metal component into fine precipitates is promoted.
[0008]
The method of modifying a membrane treated water that can solve the above problem, manganese, during the filtration operation and backwash operation of the membrane filtration device intended for the raw water containing the ion-shaped metal component iron, Hara In order to prevent the metal component in the water from being deposited as a fine precipitate in the secondary treated water after filtration, the filtration operation is performed without adding an oxidizer to the raw water during the filtration operation, and the oxidizer is added to the primary side during the backwash. Washes the primary side by feeding wash water with the addition of water, and then feeds backwash water with no oxidizer added from the secondary side of the filter membrane to peel off the cake layer and remain on the primary side It is characterized by being removed together with the oxidizing agent.
The method for modifying film treated water of the present invention, is et al., Specifically the treated water obtained from the membrane filtration unit, subsequent UF membrane, NF membrane, to form for advanced membrane filtration treatment by RO membrane It becomes.
[0009]
DETAILED DESCRIPTION OF THE INVENTION
Next, an embodiment according to the method for reforming membrane treated water of the present invention will be described with reference to FIG.
FIG. 1 exemplifies a schematic flow of a membrane filtration apparatus to which the method for reforming membrane treated water of the present invention can be applied. In the present invention, (1) filtration operation and (2) backwashing operation are performed respectively. It is characterized in that it operates under the conditions described below.
[0010]
1. Filtration operation: The filtration operation is performed without adding an oxidizing agent such as hypochlorous acid to raw water containing a small amount of ionic metal components such as manganese and iron . That is, the raw water is sent from the
[0011]
(2) Backwash operation: Immediately before or after stopping the filtration operation, a chemical containing a chlorine component such as hypochlorous acid or chlorine dioxide contained in the
[0012]
As described above, according to the operation method of the membrane filtration device of the present invention, the oxidant fed to the membrane filtration device is discharged together with the used washing water. Since chemical components in the water do not flow out to the secondary side 32, the above-described obstacles due to precipitation of minute metal deposits in the treated water on the secondary side can be completely eliminated.
[0013]
Further, as illustrated in FIG. 1, the
[0014]
Here, Table 1 illustrates the results of actual measurement of the effects of the present invention under the following conditions.
According to the results in Table 1, the FI value of the treated water of Comparative Examples 1 and 2 in which an oxidant is added to the raw water as in the conventional operating conditions indicates that the addition of the oxidant in the backwash water is the primary and secondary. Even if you replace it, it shows a high value. Further, even in the case of Comparative Example 3 in which the addition of chlorine to the raw water is omitted, the low FI value as in the present invention is not obtained.
[0015]
In addition, the test conditions of an Example and a comparative example are as follows.
The raw water used was secondary treated water of sewage (the supernatant water of the final sedimentation basin).
In the filtration step, PAC (polyaluminum chloride) was added to the raw water and agglomerated, and then membrane filtration was performed with a ceramic MF membrane in a dead-end manner. For the membrane cleaning, firstly, primary cleaning water prepared by adjusting hypochlorite as an oxidizing agent so as to have a chlorine component concentration of 50 ppm is supplied from the oxidizing
In the comparative experiment, the raw water was subjected to membrane filtration by the above method, and only membrane cleaning was changed. In other words, water obtained by adding hypochlorous water to primary washing water and backwash water and non-added water were used for membrane washing.
[0016]
The FI value (fouling index) displays the time required to obtain a predetermined amount of treated water, and is represented by the following equation.
FI = (1−T0 / T15) × 100/15
Here, T0 is the time required to initially filter 500 ml when the sample water is filtered under a pressure of 206 kPa using a 0.45 μm microfiltration membrane. T15 is the time required to filter 500 ml after continuously filtering for 15 minutes in the same state as T0. The smaller the FI value, the better (the content of fine particles is small).
[0017]
[Table 1]
[0018]
The method for modifying membrane-treated water of the present invention is a monolith, hollow fiber, tubular, honeycomb or flat membrane made of MF membrane (microfiltration membrane), UF membrane (ultrafiltration membrane) made of a polymer or ceramic material. The filter can be applied to various types of membrane filtration devices such as an external pressure type and an internal pressure type, and a filtration method such as cross flow and dead end. Moreover, it does not specifically limit as to-be-processed water. For example, wastewater and wastewater treatment such as sewage, return water, factory wastewater, waste leachate, manure, agricultural wastewater, livestock wastewater, and aquaculture wastewater, as well as water treatment can be targeted.
[0019]
【The invention's effect】
Since the method for modifying membrane-treated water of the present invention is configured as described above, a small amount of ionic metal components such as manganese and iron contained in the raw water are deposited as fine precipitates in the treated water. Can be prevented, and high-purity treated water can be provided. In addition, an advanced filtration membrane such as a UF membrane, an NF membrane, and an RO membrane can be provided in the subsequent stage, and an excellent effect is achieved that a more advanced membrane filtration system can be constructed. Therefore, the practical value of the present invention is extremely great as a method for improving membrane treated water that has solved the conventional problems.
[Brief description of the drawings]
FIG. 1 is a schematic flow diagram of a membrane filtration device for explaining an embodiment of the present invention.
FIG. 2 is a schematic flow diagram showing a main part of a conventional membrane filtration device.
[Explanation of symbols]
21 raw water tank, 22 oxidant supply tank, 23 washing water tank, 3 membrane filtration device, 30 filtration membrane, 31 primary side, 31a discharge valve, 32 secondary side, 4 altitude membrane filtration device.
Claims (2)
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JP2002307979A JP4151946B2 (en) | 2002-10-23 | 2002-10-23 | Method for reforming membrane treated water |
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JPH09122460A (en) * | 1995-10-30 | 1997-05-13 | Japan Organo Co Ltd | Cleaning method for membrane module |
JP3664835B2 (en) * | 1997-02-19 | 2005-06-29 | 日東電工株式会社 | Pretreatment system and method using spiral membrane element |
JP2000185222A (en) * | 1998-12-22 | 2000-07-04 | Tohoku Electric Power Co Inc | Chemical cleaning method for membrane separator for solid-liquid separation |
JP2001191086A (en) * | 2000-01-07 | 2001-07-17 | Kurita Water Ind Ltd | Water treating apparatus |
JP2002028456A (en) * | 2000-07-18 | 2002-01-29 | Nitto Denko Corp | Treatment system using spiral membrane module and operating method therefor |
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