JPH09155165A - Hollow fiber membrane filtration device - Google Patents
Hollow fiber membrane filtration deviceInfo
- Publication number
- JPH09155165A JPH09155165A JP34562495A JP34562495A JPH09155165A JP H09155165 A JPH09155165 A JP H09155165A JP 34562495 A JP34562495 A JP 34562495A JP 34562495 A JP34562495 A JP 34562495A JP H09155165 A JPH09155165 A JP H09155165A
- Authority
- JP
- Japan
- Prior art keywords
- hollow fiber
- fiber membrane
- water
- treated
- lower chamber
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
(57)【要約】 （修正有）
【課題】 懸濁物質の濃度が高い廃液が流入しても、１
回当りの採水量の著しい減少と洗浄周期の著しい短縮を
抑制しうる中空糸膜濾過装置を提供する。
【解決手段】 本中空糸膜濾過装置は、密閉容器１内を
上室２と下室３に区画する仕切板４と、この仕切板４に
上端が固定され且つ下端が下室へ垂下する中空糸膜モジ
ュール５とを備え、下室３に接続された流入配管６から
この室内に流入した被処理水を中空糸膜によって濾過し
て懸濁物質を除去し、その濾過水を上室２に接続された
流出配管７から流出させる装置で、下室内に流入した被
処理水を下部空間１６に導くと共にその被処理水を旋回
流及び／または下降流を生起させて懸濁物質を下部空間
内に滞留させるガイド機構１５を下室に設ける。
(57) [Summary] (Correction) [Problem] Even if waste liquid with a high concentration of suspended substances flows in, 1
Provided is a hollow fiber membrane filtration device capable of suppressing a marked decrease in the amount of water collected per cycle and a marked shortening of the washing cycle. The present hollow fiber membrane filtering apparatus includes a partition plate (4) for partitioning the inside of an airtight container (1) into an upper chamber (2) and a lower chamber (3), and a hollow in which an upper end is fixed to the partition plate (4) and a lower end hangs down to the lower chamber. With the fiber membrane module 5, the water to be treated that has flowed into this chamber from the inflow pipe 6 connected to the lower chamber 3 is filtered by a hollow fiber membrane to remove suspended substances, and the filtered water is transferred to the upper chamber 2. A device for flowing out from the connected outflow pipe 7 guides the water to be treated that has flowed into the lower chamber to the lower space 16 and causes the water to be treated to swirl and / or descend to generate suspended substances in the lower space. A guide mechanism 15 for staying in the lower chamber is provided in the lower chamber.
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、例えば原子力発電
所の放射性廃液や産業排水等、懸濁物質の濃度が高い被
処理水の処理系統に好適に用いられる中空糸膜濾過装置
に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a hollow fiber membrane filtration device suitable for use in a treatment system of treated water having a high concentration of suspended matter, such as radioactive waste liquid from a nuclear power plant or industrial wastewater.
【０００２】[0002]
【従来の技術】従来のこの種の中空糸膜濾過装置（以
下、必要に応じて単に「濾過装置」と称す。）は、例え
ば図４に示すように、密閉容器１と、この密閉容器１の
上部において上室２と下室３に区画する仕切板４と、こ
の仕切板４から下室３へ垂下する後述の中空糸膜モジュ
ール５とを備え、例えば、発電所の復水等の被処理水を
濾過して酸化鉄等の不溶性の懸濁物質を除去するように
構成されている。各中空糸膜モジュール５は仕切板４に
対してハニカム形状等の所定の幾何学模様を形成して配
置されている。そして、下室３の底部には被処理水が流
入する流入配管６が接続され、上室２の頂部には濾過水
が流出する流出配管７が接続され、各配管６、７にはバ
ルブ６Ａ、７Ａが取り付けられている。2. Description of the Related Art A conventional hollow fiber membrane filtering apparatus of this type (hereinafter, simply referred to as "filtering apparatus" if necessary) is, for example, as shown in FIG. A partition plate 4 that divides the upper chamber 2 and the lower chamber 3 at the upper part of the chamber, and a hollow fiber membrane module 5 that hangs down from the partition plate 4 to the lower chamber 3 are provided. The treated water is filtered to remove insoluble suspended matter such as iron oxide. Each hollow fiber membrane module 5 is arranged so as to form a predetermined geometric pattern such as a honeycomb shape with respect to the partition plate 4. An inflow pipe 6 through which the water to be treated flows is connected to the bottom of the lower chamber 3, and an outflow pipe 7 through which the filtered water flows out is connected to the top of the upper chamber 2, and a valve 6A is connected to each of the pipes 6 and 7. , 7A are attached.
【０００３】上記下室３内の底部近傍の中央にはバッフ
ルプレート８が被処理水の流入口に対向させて配設さ
れ、このバッフルプレート８によって下室３内へ流入し
た被処理水を分散するようにしてある。また、このバッ
フルプレート８と中空糸膜モジュール５下端との間には
分配機構９が配設され、この分配機構９によってバッフ
ルプレート８からの被処理水を一旦受け、引き続き各中
空糸膜モジュール５へ分配するようにしてある。即ち、
分配機構９は、全体が偏平なカップ状で下室３の内径よ
り縮小した外径を有する大きさに形成され、下端が開口
している。そして、分配機構９の上面には各中空糸膜モ
ジュール５に対向させた分配管１０がそれぞれ配設さ
れ、各分配管７から各中空糸膜モジュール５へ被処理水
を分配供給するようにしてある。A baffle plate 8 is disposed in the center near the bottom of the lower chamber 3 so as to face the inflow port of the water to be treated, and the baffle plate 8 disperses the water to be treated flowing into the lower chamber 3. I am doing it. A distribution mechanism 9 is arranged between the baffle plate 8 and the lower end of the hollow fiber membrane module 5, and the water to be treated from the baffle plate 8 is once received by the distribution mechanism 9, and then each hollow fiber membrane module 5 is continuously received. It is distributed to. That is,
The distribution mechanism 9 has a flat cup shape as a whole and is formed in a size having an outer diameter smaller than the inner diameter of the lower chamber 3, and has an open lower end. Then, distribution pipes 10 facing the respective hollow fiber membrane modules 5 are arranged on the upper surface of the distribution mechanism 9, and the treated water is distributed and supplied from the respective distribution pipes 7 to the respective hollow fiber membrane modules 5. is there.
【０００４】また、密閉容器１には中空糸膜モジュール
５を構成する中空糸膜に付着した懸濁物質を洗浄する際
に用いる空気配管が接続されている。この空気配管は、
上室２の頂部に接続された空気流入配管１１と、下室３
の下部に接続された空気流入配管１２と、下室３の上部
に接続された空気抜き配管１３とからなっている。そし
て、各配管１１、１２、１３にはバルブ１１Ａ、１２
Ａ、１３Ａがそれぞれ取り付けられている。また、密閉
容器１の下端にはドレン抜き配管１４が接続され、この
ドレン抜き配管１４を介して懸濁物質を含んだ洗浄廃水
を抜き取るようにしてある。尚、１４Ａはドレン抜き配
管１４に取り付けられたバルブである。Further, the closed container 1 is connected with an air pipe used for washing the suspended substance adhering to the hollow fiber membranes constituting the hollow fiber membrane module 5. This air piping is
Air inflow pipe 11 connected to the top of upper chamber 2 and lower chamber 3
And an air vent pipe 13 connected to the upper portion of the lower chamber 3. The valves 11A and 12 are provided in the pipes 11, 12 and 13, respectively.
A and 13A are attached respectively. A drain drain pipe 14 is connected to the lower end of the closed container 1, and the cleaning waste water containing suspended substances is drained through the drain drain pipe 14. 14A is a valve attached to the drain pipe 14.
【０００５】次に、上記中空糸膜モジュール５について
図５を参照しながら説明する。この中空糸膜モジュール
５は、同図に示すように、１００〜５００００本前後の
中空糸膜５１と、これらの中空糸膜５１を束ねて収納す
る保護筒５２とを備えて構成されている。各中空糸膜５
１は、例えば０.０１〜０.３μの微細孔を有する樹脂薄
膜により外径０.２〜７ｍｍ、内径０.２〜５ｍｍの中空
糸として形成されている。また、保護筒５２の上端部に
はフランジ部５２Ａが形成され、このフランジ部５２Ａ
で上記仕切板４に垂下するようにしてある。また、保護
筒５２の下端部にはスカート部５２Ｂが形成され、この
スカート部５２Ｂで洗浄時に流入した気体を捕集するよ
うにしてある。そして、保護筒５２の上端部で各中空糸
膜５１の上端部を接着剤等により束ねて接合固定した上
部接合部５３が形成され、その下端部で各中空糸膜５１
の下端部を上端部と同様に接合固定した下部接合部５４
が形成されている。上部接合部５３では各中空糸膜５１
は開口し、下部接合部５４では各中空糸膜５１は閉塞
し、濾過水が中空糸膜５１の開口から流出して上室２内
で集水するようにしてある。各中空糸膜５１の両端から
集水する場合には、それぞれの下端部も上端部と同様に
開口した状態にしておく。また、下部接合部５４には流
通孔５４Ａが形成され、流通孔５４Ａを介してスカート
部５２Ｂに捕集した気体が中空糸膜モジュール５内へ流
入するようにしてある。Next, the hollow fiber membrane module 5 will be described with reference to FIG. As shown in the figure, the hollow fiber membrane module 5 is configured to include about 100 to 50,000 hollow fiber membranes 51 and a protective cylinder 52 that bundles and stores the hollow fiber membranes 51. Each hollow fiber membrane 5
1 is formed as a hollow fiber having an outer diameter of 0.2 to 7 mm and an inner diameter of 0.2 to 5 mm, for example, by a resin thin film having fine pores of 0.01 to 0.3 μm. Further, a flange portion 52A is formed on the upper end portion of the protective cylinder 52, and the flange portion 52A
It hangs down on the partition plate 4. A skirt portion 52B is formed at the lower end of the protective cylinder 52, and the skirt portion 52B is used to collect the gas flowing in at the time of cleaning. Then, an upper joint portion 53 is formed at the upper end portion of the protective cylinder 52 by bundling and fixing the upper end portion of each hollow fiber membrane 51 with an adhesive or the like, and at the lower end portion thereof, each hollow fiber membrane 51.
Lower joint 54 with the lower end of the same joined and fixed as the upper end
Are formed. At the upper joint portion 53, each hollow fiber membrane 51
The hollow fiber membrane 51 is closed at the lower joint portion 54, and the filtered water flows out from the opening of the hollow fiber membrane 51 and collects in the upper chamber 2. When collecting water from both ends of each hollow fiber membrane 51, the lower end of each hollow fiber membrane 51 is also opened like the upper end. Further, a flow hole 54A is formed in the lower joint portion 54, and the gas collected in the skirt portion 52B flows into the hollow fiber membrane module 5 via the flow hole 54A.
【０００６】更に、上記保護筒５２の上部接合部５３の
やや下方と、下部接合部５４のやや上方にはそれぞれ流
通孔５２Ｃ、５２Ｄが形成され、これらの流通孔５２
Ｃ、５２Ｄを介して被処理水が中空糸膜モジュール５内
へ流入するようにしてある。Further, through holes 52C and 52D are formed in the protective cylinder 52 slightly below the upper joint portion 53 and slightly above the lower joint portion 54, respectively, and these through holes 52 are formed.
The water to be treated flows into the hollow fiber membrane module 5 via C and 52D.
【０００７】次に、上記濾過装置の動作について説明す
る。被処理水を濾過する場合には、流入配管６及び流出
配管７のバルブ６Ａ、７Ａをそれぞれ開放し、他のバル
ブを閉止する。この状態で被処理水を供給すると、被処
理水は流入配管６から下室３内に流入し、バッフルプレ
ート８へ衝突し、ここで被処理水が分散される。分散し
た後の被処理水は分配機構９の分配管１０及び分配機構
９の周囲から下室３内を上昇する。上昇する被処理水は
各分配管１０及び分配機構９の外周面と下室３の内周面
の隙間から保護筒５２の流通孔５２Ｃ、５２Ｄ及び流通
孔５４Ａを経由して各中空糸膜モジュール５内に流入す
る。各中空糸膜モジュール５内では被処理水はそれぞれ
の中空糸膜５１の外側から内側へ通過し、その際に被処
理水中に含まれている懸濁物質が中空糸膜５１の膜面で
捕捉される。濾過水は各中空糸膜５１の内側で得られ、
その濾過水は各中空糸膜５１内を上昇して各中空糸膜５
１の上端開口から上室２内へ集水され、更に、流出配管
７を介して所定の場所へ流出する。濾過を続行している
と、濾過装置の下室３内の被処理水の圧力と、上室２内
の濾過水の圧力との差圧が規定値以上になってその後の
濾過作用が阻害される。そこで、この時点で濾過を中止
して以下の洗浄を行う。Next, the operation of the above filtering device will be described. When filtering the water to be treated, the valves 6A and 7A of the inflow pipe 6 and the outflow pipe 7 are opened and the other valves are closed. When the water to be treated is supplied in this state, the water to be treated flows into the lower chamber 3 through the inflow pipe 6 and collides with the baffle plate 8, where the water to be treated is dispersed. The water to be treated after being dispersed rises in the lower chamber 3 from around the distribution pipe 10 of the distribution mechanism 9 and the distribution mechanism 9. The rising water to be treated is passed through the clearances between the outer peripheral surface of each distribution pipe 10 and the distribution mechanism 9 and the inner peripheral surface of the lower chamber 3 through the flow holes 52C and 52D of the protective cylinder 52 and the flow hole 54A, and each hollow fiber membrane module. Inflow into 5. In each hollow fiber membrane module 5, the water to be treated passes from the outer side to the inner side of the respective hollow fiber membranes 51, and at that time, suspended substances contained in the water to be treated are captured by the membrane surface of the hollow fiber membranes 51. To be done. The filtered water is obtained inside each hollow fiber membrane 51,
The filtered water ascends in each hollow fiber membrane 51 and each hollow fiber membrane 5
Water is collected into the upper chamber 2 from the upper end opening of 1, and further flows out to a predetermined place through the outflow pipe 7. When the filtration is continued, the pressure difference between the pressure of the water to be treated in the lower chamber 3 of the filtering device and the pressure of the filtered water in the upper chamber 2 becomes equal to or more than the specified value, and the subsequent filtering action is hindered. It Therefore, at this point, the filtration is stopped and the following washing is performed.
【０００８】濾過装置の洗浄は、圧縮空気を下室３内に
供給し、下室３内で生成する気泡で水をスクラビングす
ることによって行う。即ち、流入配管６及び流出配管７
のバルブ６Ａ、７Ａを閉止し、下室３内及び上室２内が
満水状態のまま、空気流入配管１２及び空気抜き配管１
３のバルブ１２Ａ、１３Ａを開放し、空気流入配管１２
から下室３内へ圧縮空気を供給する。下室３内に流入し
た空気は、気泡となって下室３内を上昇し、分配機構９
によって受け止められ、それが溜まって分配機構９にお
いて空気層を形成する。引き続き、気泡が分配管１０の
側部に設けてある図示しない気泡流入孔から保護筒５２
のスカート部５２Ｂ及び下部接合部の流通孔５４Ａを経
由して各中空糸膜モジュール５内に流入する。各中空糸
膜モジュール５内では気泡が上昇する際に水を気泡によ
り攪拌し、この攪拌作用により各中空糸膜５１で捕捉さ
れた懸濁物質を剥離する。剥離した懸濁物質は各中空糸
膜モジュール５内の水や気泡に随伴して流通孔５２Ｃ、
５２Ｄから外部へ流出し洗浄廃水として下室３内に留ま
る。また、各中空糸膜モジュール５から流出した気泡は
空気抜き配管１３を介して濾過装置外へ流出する。Cleaning of the filtration device is performed by supplying compressed air into the lower chamber 3 and scrubbing water with the bubbles generated in the lower chamber 3. That is, the inflow pipe 6 and the outflow pipe 7
The valves 6A and 7A are closed and the inside of the lower chamber 3 and the inside of the upper chamber 2 remain full, and the air inflow pipe 12 and the air vent pipe 1
The valves 12A and 13A of No. 3 are opened, and the air inflow pipe 12
To supply the compressed air into the lower chamber 3. The air that has flowed into the lower chamber 3 becomes bubbles and rises in the lower chamber 3 to cause the distribution mechanism 9
It is received by and collects and forms an air layer in the distribution mechanism 9. Subsequently, bubbles are protected from the bubble inlet hole (not shown) provided on the side portion of the distribution pipe 10 by the protective cylinder 52.
It flows into each hollow fiber membrane module 5 through the skirt portion 52B and the flow hole 54A of the lower joint portion. In each hollow fiber membrane module 5, when the bubbles rise, water is stirred by the bubbles, and the suspended substance captured by each hollow fiber membrane 51 is peeled off by this stirring action. The separated suspended solids accompany water and air bubbles in each hollow fiber membrane module 5 and flow holes 52C,
It flows out from 52D to the outside and remains in the lower chamber 3 as cleaning wastewater. Further, the air bubbles that have flowed out from each hollow fiber membrane module 5 flow out to the outside of the filtration device through the air vent pipe 13.
【０００９】更に、上述のスクラビングによる洗浄を行
った後、空気抜き配管１３のバルブ１３Ａを開放したま
まの状態で空気流入配管１２のバルブ１２Ａを閉止し、
ドレン抜き配管１４のバルブ１４Ａを開放すると、下室
３内の洗浄廃水は水圧によりドレン抜き配管１４から外
部へ流出する。これにより各中空糸膜モジュール５の濾
過機能を回復させることができる。この際、空気流入配
管１２及び／または空気抜き配管１３から圧縮空気を供
給すれば、その空気圧により洗浄廃水の流出を促進して
急速抜き出しを行うことができる。Further, after cleaning by scrubbing as described above, the valve 12A of the air inflow pipe 12 is closed while the valve 13A of the air vent pipe 13 is left open,
When the valve 14A of the drainage pipe 14 is opened, the cleaning wastewater in the lower chamber 3 flows out from the drainage pipe 14 to the outside by water pressure. Thereby, the filtration function of each hollow fiber membrane module 5 can be restored. At this time, if compressed air is supplied from the air inflow pipe 12 and / or the air bleed pipe 13, the air pressure can accelerate the outflow of the cleaning wastewater, thereby enabling rapid withdrawal.
【００１０】また、スクラビング中あるいはその前後
に、空気流入配管１１及び空気抜き配管１３及びドレン
抜き配管１４のバルブ１１Ａ、１３Ａ、１４Ａをそれぞ
れ開放し、その他のバルブを閉止した状態で、圧縮空気
を空気流入配管１１から供給すれば、圧縮空気が上室２
へ流入し、その空気圧によって上室２内に残留する濾過
水を各中空糸膜５１内へ逆流させると、その濾過水は各
中空糸膜５１の内側から外側へ流出し、これにより各中
空糸膜５１の微細孔に目詰まりしている懸濁物質の微粒
子を洗い落とし、その洗浄廃水をドレン抜き配管１４か
ら抜き出すことができる。During or before and after scrubbing, the compressed air is blown with air while the valves 11A, 13A and 14A of the air inflow pipe 11, the air vent pipe 13 and the drain vent pipe 14 are opened and the other valves are closed. If it is supplied from the inflow pipe 11, compressed air will be supplied to the upper chamber 2.
When the filtered water remaining in the upper chamber 2 is caused to flow back into each hollow fiber membrane 51 due to the air pressure thereof, the filtered water flows out from the inside of each hollow fiber membrane 51 to the outside, whereby each hollow fiber The fine particles of the suspended substance clogging the fine pores of the membrane 51 can be washed off, and the cleaning wastewater can be extracted from the drainage pipe 14.
【００１１】ところで、上述の洗浄頻度は被処理水中に
含まれている懸濁物質の濃度及び性状に従って変動し、
また、洗浄廃水の発生量も被処理水中に含まれている懸
濁物質の濃度及び性状に従って変動する。即ち、被処理
水中に含有される懸濁物質の濃度が高く、あるいは懸濁
物質の濾過性が悪い場合には、中空糸膜モジュール５の
中空糸膜５１が短時間で目詰まりを起こし、濾過中の差
圧上昇が早く、濾過水の採水量が減少し、洗浄周期が短
くなり、ひいては洗浄廃水の発生量が増加する。そのた
め、原子力発電所の放射性廃液などのようにその中に含
まれる懸濁物質の濃度が高い系統に上記濾過装置を適用
する場合には、発電所の復水系など懸濁物質の濃度が低
い系統に上記濾過装置を適用する場合の１／２〜１／３
という低い濾過速度に設定している。By the way, the above-mentioned cleaning frequency varies depending on the concentration and properties of the suspended matter contained in the water to be treated,
In addition, the amount of cleaning wastewater generated also varies according to the concentration and properties of the suspended substances contained in the water to be treated. That is, when the concentration of the suspended matter contained in the water to be treated is high or the filterability of the suspended matter is poor, the hollow fiber membranes 51 of the hollow fiber membrane module 5 are clogged in a short time, and filtration is performed. The pressure difference in the inside rises quickly, the amount of filtered water collected decreases, the cleaning cycle shortens, and the amount of cleaning wastewater generated increases. Therefore, when applying the above filtering device to a system with a high concentration of suspended matter contained therein, such as radioactive waste liquid from a nuclear power plant, a system with a low concentration of suspended matter such as a condensate system of a power plant 1/2 to 1/3 of the case where the above filtering device is applied to
Is set to a low filtration rate.
【００１２】[0012]
【発明が解決しようとする課題】しかしながら、一般的
に、廃液中の懸濁物質は性状や濃度の変動が著しく、例
えば、原子力発電所の放射性廃液の場合には、懸濁物質
の濃度が数ｐｐｍ〜数１００ｐｐｍの範囲で大きく変動
する。そのため、従来の技術では例えば懸濁物質の濃度
が平均的な濃度で数１０ｐｐｍの廃液が流入する場合に
は、数時間の採水が可能で、濾過装置の洗浄頻度が１回
／日程度であるが、その濃度が最大濃度級の数１００ｐ
ｐｍ程度に達した廃液が流入する場合には、採水時間が
極端に短く１時間にも満たず、採水量も極端に少なくな
り、濾過装置の洗浄頻度が極端に高くなって数回／日程
度になって所定の処理を行うのに長時間を要したり、洗
浄廃水量が増加してその処理が困難になったりして運転
員の負担が増大するという課題があった。However, in general, the properties and concentration of suspended solids in a waste liquid vary significantly. For example, in the case of radioactive waste liquid of a nuclear power plant, the concentration of suspended solids is a few. It fluctuates greatly in the range of ppm to several 100 ppm. Therefore, in the conventional technique, for example, when a waste liquid having an average concentration of suspended substances of several tens of ppm flows in, it is possible to collect water for several hours and to wash the filter device once or about once a day. There is a maximum concentration of several 100p
When the waste liquid reaches about pm, the sampling time is extremely short, less than 1 hour, the sampling amount is extremely small, and the cleaning frequency of the filtering device is extremely high, and the sampling frequency is several times / day. However, there is a problem in that it takes a long time to perform a predetermined treatment due to a certain degree, or the amount of cleaning wastewater increases and the treatment becomes difficult, which increases the burden on the operator.
【００１３】一方、従来の濾過装置を用いて最大級の濃
度に対する採水量を確保するためには、濾過流速を下
げ、差圧上昇を低減すれば良いが、そのためには中空糸
膜モジュールの本数を増加する必要を生じてしまい、勢
い濾過装置が大型化すると共にコスト高を招いて経済性
を損なうことになる。On the other hand, in order to secure the amount of water to be collected for the maximum concentration by using the conventional filtration device, the filtration flow rate may be decreased to reduce the increase in differential pressure. To this end, the number of hollow fiber membrane modules is required. Therefore, it is necessary to increase the cost, the size of the vibrating filter becomes large, the cost becomes high, and the economical efficiency is impaired.
【００１４】本発明は、上記課題を解決するためになさ
れたもので、懸濁物質の濃度が高い廃液が流入しても同
じ本数の中空糸膜モジュールでも１回当たりの採水量の
著しい減少と洗浄周期の著しい短縮を抑制することがで
きる中空糸膜濾過装置を提供することを目的としてい
る。The present invention has been made in order to solve the above problems, and even if a waste liquid having a high concentration of suspended substances flows in, even if the same number of hollow fiber membrane modules are used, the amount of water taken per one time is significantly reduced. An object of the present invention is to provide a hollow fiber membrane filtration device capable of suppressing a significant reduction in the cleaning cycle.
【００１５】[0015]
【課題を解決するための手段】本発明者らは、高濃度の
懸濁物質を含む被処理水の濾過作用について種々検討し
た結果、懸濁物質の濃度が高い場合には一般的に懸濁物
質の粒径が大きく、更にフロック化し易いことに着目
し、下室内で高濃度の懸濁物質を含む被処理水に特定の
流れを生起させることによって中空糸膜モジュールに達
する前に、被処理水中からある程度の懸濁物質を除去で
き、中空糸膜モジュールの負荷を低減し、もって１回当
たりの採水量が増加し、洗浄頻度を低下し得ることを知
見した。Means for Solving the Problems As a result of various studies on the filtering action of water to be treated containing a high concentration of suspended solids, the present inventors have found that when the concentration of suspended solids is high, it is generally suspended. Focusing on the fact that the particle size of the substance is large and it is easy to form flocs, the treated water containing a high concentration of suspended substances is caused to generate a specific flow in the lower chamber before it reaches the hollow fiber membrane module. It has been found that a certain amount of suspended solids can be removed from water, the load on the hollow fiber membrane module can be reduced, the amount of water taken per time can be increased, and the cleaning frequency can be reduced.
【００１６】本発明は上記知見に基づいてなされたもの
で、請求項１に記載の中空糸膜濾過装置は、密閉容器内
を上室と下室に区画する仕切板と、この仕切板に上端が
固定され且つ下端が下室へ垂下する中空糸膜モジュール
とを備え、上記下室に形成された流入口からこの室内に
流入した被処理水を上記中空糸膜モジュールを構成する
多数本の中空糸膜によって濾過して懸濁物質を除去し、
その濾過水を上記上室に形成された流出口から流出させ
る中空糸膜濾過装置において、上記下室内に流入した被
処理水を上記中空糸膜モジュール下端と上記密閉容器の
底部との間に設けた下部空間に導くと共にその被処理水
を上記中空糸膜モジュールに流入させる前に旋回流及び
／または下降流を生起させて懸濁物質を上記下部空間内
に滞留させる懸濁物質分離手段を上記下室に設けたこと
を特徴とするものである。The present invention has been made on the basis of the above findings, and the hollow fiber membrane filtering apparatus according to claim 1 is such that a partition plate for partitioning the inside of the closed container into an upper chamber and a lower chamber, and an upper end of this partition plate. And a hollow fiber membrane module whose lower end hangs down to the lower chamber, and the water to be treated that has flowed into the chamber from the inlet formed in the lower chamber is formed into a large number of hollow fibers constituting the hollow fiber membrane module. Filtered through a thread membrane to remove suspended matter,
In the hollow fiber membrane filtration device for causing the filtered water to flow out from the outlet formed in the upper chamber, the water to be treated that has flowed into the lower chamber is provided between the lower end of the hollow fiber membrane module and the bottom of the closed container. The suspended substance separating means for guiding the treated water to the lower space and causing the swirling flow and / or the downward flow to cause the suspended substance to stay in the lower space before the treated water flows into the hollow fiber membrane module. It is characterized by being installed in the lower chamber.
【００１７】また、本発明の請求項２に記載の中空糸膜
濾過装置は、請求項１に記載の発明において、上記懸濁
物質分離手段として、上記下室内周面と上記中空糸膜モ
ジュール群の間に設けられた筒状の邪魔板と、この邪魔
板の上端と上記下室内周面間の隙間を塞ぐ邪魔板とを備
えたことを特徴とするものである。The hollow fiber membrane filtering device according to a second aspect of the present invention is the hollow fiber membrane filtering device according to the first aspect of the invention, wherein the suspended substance separating means is the lower chamber peripheral surface and the hollow fiber membrane module group. A tubular baffle plate provided between the baffle plate and a baffle plate that closes a gap between the upper end of the baffle plate and the peripheral surface of the lower chamber.
【００１８】また、本発明の請求項３に記載の中空糸膜
濾過装置は、請求項１に記載の発明において、上記懸濁
物質分離手段として、上記下部空間をサイクロンセパレ
ータとして構成したことを特徴とするものである。The hollow fiber membrane filtering device according to a third aspect of the present invention is characterized in that, in the first aspect of the invention, the lower space is constituted as a cyclone separator as the suspended substance separating means. It is what
【００１９】[0019]
【発明の実施の形態】以下、図１〜図３に示す実施形態
に基づいて従来と同一部分または相当部分には同一符号
を付して本発明の特徴を中心にして説明する。尚、各図
中、図１は本発明の中空糸膜濾過装置の一実施形態の軸
方向断面を示す模式図、図２は本発明の中空糸膜濾過装
置の他の実施形態の軸方向断面を示す模式図、図３は、
図１に示す中空糸膜濾過装置の採水量と従来の中空糸膜
濾過装置の採水量とを比較したグラフである。BEST MODE FOR CARRYING OUT THE INVENTION Hereinafter, based on the embodiments shown in FIGS. 1 to 3, the same parts or corresponding parts as in the prior art will be designated by the same reference numerals, and the description will focus on the characteristics of the present invention. In each drawing, FIG. 1 is a schematic view showing an axial cross section of an embodiment of the hollow fiber membrane filtering device of the present invention, and FIG. 2 is an axial cross section of another embodiment of the hollow fiber membrane filtering device of the present invention. 3 is a schematic diagram showing
It is the graph which compared the water sampling amount of the hollow fiber membrane filtering apparatus shown in FIG. 1, and the conventional hollow fiber membrane filtering apparatus.
【００２０】第１の実施形態の濾過装置は、図１に示す
ように、密閉容器１と、この密閉容器１内を上室２と下
室３に区画する仕切板４と、この仕切板４に上端が固定
され且つ下端が下室３側へ垂下する複数の中空糸膜モジ
ュール５とを備え、下室３に形成された流入口（流入配
管６）からこの室３内に流入した被処理水、例えば原子
力発電所で発生する放射性廃液からなる原水を各中空糸
膜モジュール５を構成する多数本の中空糸膜５１（図５
参照）によって濾過して懸濁物質を除去し、濾過水を上
室２に形成された流出口（流出配管７）から流出させる
ように構成されている。As shown in FIG. 1, the filtration apparatus of the first embodiment has a closed container 1, a partition plate 4 for partitioning the closed container 1 into an upper chamber 2 and a lower chamber 3, and a partition plate 4. A plurality of hollow fiber membrane modules 5 each having an upper end fixed to the lower chamber 3 and a lower end hanging toward the lower chamber 3 side, and an object to be treated which has flowed into the chamber 3 from an inlet port (inflow pipe 6) formed in the lower chamber 3. A large number of hollow fiber membranes 51 (FIG. 5) that constitute each hollow fiber membrane module 5 are made of water, for example, raw water composed of radioactive waste liquid generated in a nuclear power plant.
(See reference) to remove suspended substances, and the filtered water is made to flow out from the outlet (outflow pipe 7) formed in the upper chamber 2.
【００２１】上記下室３には、流入配管６から下室３内
に流入した被処理水が中空糸膜モジュール５に流入する
前に、一旦中空糸膜モジュール５下端と密閉容器１の底
部との間に形成された下部空間１６に被処理水を導くと
共にその被処理水に旋回流及び／または下降流を生起さ
せて下部空間１６で懸濁物質を滞留させるガイド機構１
５が懸濁物質分離手段として設けられている。このガイ
ド機構１５は、下室３の内周面と中空糸膜モジュール５
からなるモジュール群の周囲の間に設けられた筒状の邪
魔板１５Ａと、この邪魔板１５Ａの上端と下室３の内周
面間の隙間を塞ぐ環状の邪魔板１５Ｂとを備えている。
また、邪魔板１５Ａは、分配機構９の外周面より外寄り
に位置し、この外周壁の下端と同一かそれよりも低い高
さに調整することが好ましい。従って、下室３の周壁
面、邪魔板１５Ａ及び環状の邪魔板１５Ｂによって上端
が閉塞され下端が開口された筒状の隙間空間１５Ｃを形
成している。また、隙間空間１５Ｃを形成する下室３の
周壁上端部には流入配管６が接続されている。この流入
配管６は上記周壁に対して法線方向に取り付けても良
く、また、上記周壁に対して接線方向に取り付けても良
い。更に、流入配管６は斜め下方へ傾斜させて上記周壁
に取り付けても良い。このような接続形態の流入配管６
から隙間空間１５Ｃへ流入した原水は、その空間１５Ｃ
内で旋回流及び／または下降流を生起し、隙間空間１５
Ｃに従って下室３の底部へ到達するようにしてある。
尚、上記邪魔板１５Ａはバッフルプレートの機能をも有
するため、従来のバッフルプレート８は省略してある。
その他は、従来の濾過装置に準じて構成されている。Before the water to be treated, which has flowed into the lower chamber 3 from the inflow pipe 6, flows into the lower chamber 3, the lower end of the hollow fiber membrane module 5 and the bottom of the closed container 1 are temporarily provided before the water to be treated flows into the hollow fiber membrane module 5. A guide mechanism 1 for guiding the water to be treated to the lower space 16 formed between the water and causing a swirl flow and / or a downward flow in the water to be treated to retain the suspended substance in the lower space 16.
5 is provided as a suspended solid separation means. The guide mechanism 15 includes the inner peripheral surface of the lower chamber 3 and the hollow fiber membrane module 5.
A cylindrical baffle plate 15A provided between the periphery of the module group consisting of and an annular baffle plate 15B for closing a gap between the upper end of the baffle plate 15A and the inner peripheral surface of the lower chamber 3.
Further, it is preferable that the baffle plate 15A is located outside the outer peripheral surface of the distribution mechanism 9 and is adjusted to have a height equal to or lower than the lower end of the outer peripheral wall. Therefore, the peripheral wall surface of the lower chamber 3, the baffle plate 15A and the annular baffle plate 15B form a cylindrical clearance space 15C having an upper end closed and a lower end opened. Further, an inflow pipe 6 is connected to an upper end portion of the peripheral wall of the lower chamber 3 forming the clearance space 15C. The inflow pipe 6 may be attached to the peripheral wall in a normal direction, or may be attached to the peripheral wall in a tangential direction. Further, the inflow pipe 6 may be attached obliquely downward to the peripheral wall. Inflow pipe 6 having such a connection form
Raw water flowing into the interstitial space 15C from the
A swirl flow and / or a downward flow is generated in the gap space 15
According to C, the bottom of the lower chamber 3 is reached.
Since the baffle plate 15A also has the function of a baffle plate, the conventional baffle plate 8 is omitted.
Others are configured according to the conventional filtration device.
【００２２】次に、動作について説明する。まず、被処
理水を濾過する場合について説明する。被処理水を濾過
する場合には、流入配管６及び流出配管７のバルブ６
Ａ、７Ａをそれぞれ開放し、他のバルブを閉止する。こ
の状態で被処理水を供給すると、被処理水は流入配管６
から下室３内に流入する。流入した被処理水は隙間空間
１５Ｃにおいて旋回流及び／または下降流を作って隙間
空間１５Ｃに従ってフロック形成に必要な流速に低下し
つつ下方へ流れる。この間、被処理水中の懸濁物質は隙
間空間１５Ｃ内の適度な流れによる適度な攪拌の作用に
よりフロック形成が促進されて沈降分離し易くなる。
尚、フロック形成に適切な流速としては一般的に０.７
５ｍ／秒以下が望ましく、０.４ｍ／秒以下がより望ま
しいが、最適な流速は被処理水の性状に応じて試験を行
って求めるのが一般的である。また、隙間空間１５Ｃ内
の被処理水は下方に直線的に流すよりも旋回流を生起さ
せて螺旋状に下方へ流す方がフロック形成をより促進し
易くなるのでより好適である。被処理水が隙間空間１５
Ｃから流出すると、この被処理水は分配機構９の下部空
間１６へ一気に拡散して流速が急激に減速され、下室３
の底面に達すると、下部空間１６において上昇流に転ず
る。この下部空間１６において懸濁物質の流速は被処理
水と共に減速されるが被処理水との比重差に基づく慣性
力で懸濁物質の沈降が促進され、懸濁物質の濃度が高け
れば高いほど懸濁物質がフロック化して被処理水から沈
降分離し易くなって下部空間１６の底部に滞留し、中空
糸膜モジュール５に対する負荷を低減する。Next, the operation will be described. First, the case of filtering the water to be treated will be described. When filtering the water to be treated, the valves 6 of the inflow pipe 6 and the outflow pipe 7
Open A and 7A respectively and close the other valves. When the water to be treated is supplied in this state, the water to be treated flows into the inflow pipe 6
Flows into the lower chamber 3. The water to be treated that has flowed in creates a swirling flow and / or a downward flow in the clearance space 15C and flows downward while the flow speed is reduced to a flow rate required for flock formation in accordance with the clearance space 15C. During this period, the suspended substances in the water to be treated are easily agitated by the action of appropriate agitation due to the appropriate flow in the interstitial space 15C to facilitate sedimentation and separation.
In addition, the flow velocity suitable for flock formation is generally 0.7.
The flow velocity is preferably 5 m / sec or less, more preferably 0.4 m / sec or less, but the optimum flow velocity is generally determined by conducting a test according to the properties of the water to be treated. In addition, it is more preferable that the water to be treated in the clearance space 15C causes a swirling flow to flow downward spirally rather than linearly flow downward because it facilitates flock formation. Water to be treated has a gap space 15
When it flows out from C, this water to be treated diffuses into the lower space 16 of the distribution mechanism 9 all at once, and the flow velocity is rapidly reduced.
When it reaches the bottom surface of the lower space 16, it changes to an upward flow in the lower space 16. In this lower space 16, the flow velocity of the suspended substance is reduced with the water to be treated, but the sedimentation of the suspended substance is promoted by the inertial force based on the difference in specific gravity from the water to be treated, and the higher the concentration of the suspended substance, the higher the concentration. The suspended substance becomes flocs and easily settles and separates from the water to be treated and stays at the bottom of the lower space 16 to reduce the load on the hollow fiber membrane module 5.
【００２３】このようにして懸濁物質が部分的に被処理
水から分離し、懸濁物質の濃度がある程度低減した被処
理水は分配機構９の各分配管１０及び分配機構９の外周
面と下室３の周壁の隙間から上昇し、保護筒５２の流通
孔５２Ｃ、５２Ｄ及び下部接合部の流通孔５４Ａを介し
て中空糸膜モジュール５内に流入する。各中空糸膜モジ
ュール５内では被処理水はそれぞれの中空糸膜５１の外
側から内側へ通過し、その際に被処理水中に含まれてい
る懸濁物質が中空糸膜５１の膜面で捕捉される。濾過水
は各中空糸膜５１の内側で得られ、その濾過水は各中空
糸膜５１内を上昇して各中空糸膜５１の上端開口から上
室２内へ集水され、更に、流出配管７を介して所定の場
所へ流出する。濾過を続行していると、濾過装置の下室
３内の被処理水の圧力と、上室２内の濾過水の圧力との
差圧が規定値以上になってその後の濾過作用が阻害され
ると、この時点で従来と同様の方法によって濾過装置を
洗浄する。In this way, the suspended solids are partially separated from the water to be treated, and the water to be treated in which the concentration of the suspended solids is reduced to some extent is distributed to the respective distribution pipes 10 of the distribution mechanism 9 and the outer peripheral surface of the distribution mechanism 9. It rises from the gap of the peripheral wall of the lower chamber 3 and flows into the hollow fiber membrane module 5 through the flow holes 52C and 52D of the protective cylinder 52 and the flow hole 54A of the lower joint. In each hollow fiber membrane module 5, the water to be treated passes from the outer side to the inner side of the respective hollow fiber membranes 51, and at that time, suspended substances contained in the water to be treated are captured by the membrane surface of the hollow fiber membranes 51. To be done. The filtered water is obtained inside each hollow fiber membrane 51, and the filtered water rises in each hollow fiber membrane 51 and is collected into the upper chamber 2 from the upper end opening of each hollow fiber membrane 51. It flows out to a predetermined place through 7. When the filtration is continued, the pressure difference between the pressure of the water to be treated in the lower chamber 3 of the filtering device and the pressure of the filtered water in the upper chamber 2 becomes equal to or more than the specified value, and the subsequent filtering action is hindered. Then, at this point, the filtration device is washed by a method similar to the conventional one.
【００２４】以上説明したように本実施形態によれば、
下室３内に流入する被処理水を中空糸膜モジュール５内
に流入させる前に下部空間１６内に導くと共に旋回流及
び／または下降流を生起させるガイド機構１５を下室３
内に設け、しかも、このガイド機構１５は、下室３の周
壁面と複数の中空糸膜モジュール５からなるモジュール
群の間に設けられた筒状の邪魔板１５Ａと、この邪魔板
１５Ａの上端と下室３の周壁間の隙間空間１５Ｃの上端
を塞ぐ邪魔板１５Ｂとを備えているため、被処理水が各
中空糸膜モジュール５へ到達する前に下部空間１６にお
いて懸濁物質の一部を沈降させて被処理水から分離する
ことができ、その結果、懸濁物質の濃度が高い被処理水
であっても中空糸膜モジュール５の本数を増加すること
なく、１回当たりの採水量を極端に減少せず、洗浄周期
を極端に短縮することがない。従って、オペレータの労
働負荷を格段に軽減することができる。As described above, according to this embodiment,
The guide mechanism 15 that guides the water to be treated flowing into the lower chamber 3 into the lower space 16 before causing it to flow into the hollow fiber membrane module 5 and causes a swirling flow and / or a downward flow is installed in the lower chamber 3.
Further, the guide mechanism 15 is provided inside the tubular baffle plate 15A provided between the peripheral wall surface of the lower chamber 3 and the module group including the plurality of hollow fiber membrane modules 5, and the upper end of the baffle plate 15A. And a baffle plate 15B that closes the upper end of the clearance space 15C between the peripheral walls of the lower chamber 3, so that a portion of the suspended substance in the lower space 16 before the water to be treated reaches each hollow fiber membrane module 5. Can be settled and separated from the water to be treated, and as a result, even if the water to be treated has a high concentration of suspended solids, the amount of water taken per time can be increased without increasing the number of hollow fiber membrane modules 5. Is not extremely reduced, and the cleaning cycle is not extremely shortened. Therefore, the workload of the operator can be significantly reduced.
【００２５】また、図２は他の実施形態の濾過装置を示
す図である。本実施形態の濾過装置は、同図に示すよう
に、下部空間１６をサイクロンセパレータ１７として構
成した以外は図４に示す濾過装置と同様に構成されてい
る。このサクロンセパレータ１７は、周知のように、直
胴部１７Ａと、この直胴部１７Ａの上端を閉塞する天蓋
部１７Ｂと、この天蓋部１７Ｂの中央開口に取付られ、
被処理水の下室３内への流出部となる筒状部材１７Ｃ
と、上記直胴部１７Ａの下端に連設されたホッパー部１
７Ｄとを備え、懸濁物質分離手段として構成されてい
る。そして、直胴部１７Ａの上部に被処理水の流入配管
６が接続され、ホッパー部１７Ｄの下端にドレン抜き配
管１４が接続されている。流入配管６は直胴部１７Ａに
対して接線方向に接続され、被処理水が直胴部１７Ａと
筒状部材１７Ｃ間の空間に旋回流を作るように流入する
ようにしてある。FIG. 2 is a view showing a filter device according to another embodiment. As shown in the figure, the filtering device of the present embodiment is configured similarly to the filtering device shown in FIG. 4, except that the lower space 16 is configured as a cyclone separator 17. As is well known, the SACRON separator 17 is attached to a straight body portion 17A, a canopy portion 17B that closes the upper end of the straight body portion 17A, and a central opening of the canopy portion 17B.
Cylindrical member 17C serving as an outflow portion into the lower chamber 3 of the water to be treated
And the hopper portion 1 which is continuously provided at the lower end of the straight body portion 17A.
7D, and is configured as a suspended substance separating means. The inflow pipe 6 of the water to be treated is connected to the upper part of the straight body part 17A, and the drain pipe 14 is connected to the lower end of the hopper part 17D. The inflow pipe 6 is tangentially connected to the straight body portion 17A so that the water to be treated flows into the space between the straight body portion 17A and the tubular member 17C so as to create a swirling flow.
【００２６】次に、本実施形態の特徴的動作について説
明する。被処理水を濾過する場合には、流入配管６及び
流出配管７のバルブ６Ａ、７Ａをそれぞれ開放し、他の
バルブを閉止する。この状態で被処理水を供給すると、
被処理水は流入配管６からサイクロンセパレータ１７内
に流入する。流入した被処理水は直胴部１７Ａと筒状部
材１７Ｃ間の空間１５Ｃにおいて旋回流及び／または下
降流を作ってその空間に従って流れ、ホッパー部１７Ｄ
へ到達するとホッパー部１７Ｄにおいて懸濁物質が被処
理水から分離し、懸濁物質の沈降が促進され、懸濁物質
の濃度が高ければ高いほど懸濁物質の多くが沈降して被
処理水から分離され、ホッパー部１７Ｄに滞留し、中空
糸膜モジュール５に対する負荷を低減する。Next, the characteristic operation of this embodiment will be described. When filtering the water to be treated, the valves 6A and 7A of the inflow pipe 6 and the outflow pipe 7 are opened and the other valves are closed. If the water to be treated is supplied in this state,
The water to be treated flows into the cyclone separator 17 from the inflow pipe 6. The water to be treated that has flowed in creates a swirling flow and / or a downward flow in a space 15C between the straight body portion 17A and the tubular member 17C and flows according to the space, and the hopper portion 17D
When the water reaches the hopper 17D, the suspended solids are separated from the water to be treated, and the sedimentation of the suspended solids is promoted. It is separated and stays in the hopper portion 17D to reduce the load on the hollow fiber membrane module 5.
【００２７】このようにして懸濁物質が部分的に被処理
水から分離し、懸濁物質の濃度がある程度低減した被処
理水はその上昇流で分配機構９の各分配管１０からそれ
ぞれの対応する保護筒５２のスカート部５２Ｂ及び下部
接合部の流通孔５４Ａを介して中空糸膜モジュール５内
に流入し、後は図１に示す濾過装置と同様にして濾過さ
れ、濾過水が上室２内を経由して流出配管７から所定の
場所へ流出する。濾過後の洗浄操作も図１に示す場合と
同様に行う。In this way, the suspended solids are partially separated from the water to be treated, and the water to be treated in which the concentration of the suspended solids has been reduced to some extent is dealt with by the ascending flow from the respective distribution pipes 10 of the distribution mechanism 9. Through the skirt portion 52B of the protective cylinder 52 and the flow hole 54A of the lower joint portion, and then flows into the hollow fiber membrane module 5, and thereafter is filtered in the same manner as the filtering device shown in FIG. It flows out from the outflow pipe 7 to a predetermined place via the inside. The washing operation after filtration is performed in the same manner as in the case shown in FIG.
【００２８】以上説明したように本実施形態によれば、
下室３内に流入する被処理水を中空糸膜モジュール５内
に流入させる前に中空糸膜モジュール５下端と密閉容器
１の底部との間に設けた下部空間１６内に導くと共に旋
回流及び／または下降流を生起させて懸濁物質を被処理
水から分離させる懸濁物質分離手段を下室３内に設け、
しかも、この懸濁物質分離手段として、下室３の下端に
連設されたサイクロンセパレータ１７を設けたため、被
処理水が各中空糸膜モジュール５へ到達する前にサイク
ロンセパレータ１７により懸濁物質の一部を沈降させて
被処理水から分離することができ、前述の実施形態と同
様の作用効果を期することができる。As described above, according to this embodiment,
Before the water to be treated flowing into the lower chamber 3 is introduced into the hollow fiber membrane module 5, it is guided into the lower space 16 provided between the lower end of the hollow fiber membrane module 5 and the bottom of the closed container 1, and the swirling flow and And / or a suspended substance separating means for causing a descending flow to separate suspended substances from the water to be treated is provided in the lower chamber 3,
In addition, since the cyclone separator 17 connected to the lower end of the lower chamber 3 is provided as the suspended substance separating means, the suspended substance is separated by the cyclone separator 17 before the water to be treated reaches each hollow fiber membrane module 5. A part of the water can be settled and separated from the water to be treated, and the same effect as that of the above-described embodiment can be expected.
【００２９】[0029]
【実施例】本実施例では、下記仕様の図１に示す本発明
の濾過装置を用いて懸濁物質の濃度を異にする２種類の
廃液を被処理水として下記の条件で濾過を行った。ま
た、本実施例に対する比較例として邪魔板を有しない図
４に示す従来の濾過装置を用いて本実施例と同様の条件
で濾過を行った。そして、被処理水の採水量及び洗浄周
期を図３に示した。尚、図３では実線で示すものが本実
施例の結果を示し、破線で示すものが比較例の結果を示
している。EXAMPLES In this example, two kinds of waste liquids having different concentrations of suspended substances were treated as water to be treated and filtered under the following conditions by using the filtration apparatus of the present invention having the following specifications shown in FIG. . Further, as a comparative example to this example, filtration was performed under the same conditions as in this example using a conventional filtration device having no baffle shown in FIG. The amount of water to be treated and the cleaning cycle are shown in FIG. In FIG. 3, the solid line shows the result of this example, and the broken line shows the result of the comparative example.
【００３０】図３に示す結果によれば、被処理水の懸濁
物質の濃度が５０ｐｐｍの時には、本実施例の場合には
比較例の場合と比較して１回当たりの採水量が漸増し、
洗浄周期が徐々に長くなっていることが判る。また、懸
濁物質の濃度が５倍の２５０ｐｐｍという高濃度になる
と、比較例では差圧上昇の速度も５倍になるため、洗浄
サイクル当たりの採水量は１／５に低下する。これに対
して、本実施例では懸濁物質の濃度が５倍になっても、
洗浄サイクル当たりの採水量の低下は１／２程度に抑制
できる。換言すれば、同一採水量であれば、本実施例で
は１回の洗浄で済むところ、比較例では３回の洗浄が必
要になり、洗浄周期が大幅に長くなっていることが判
る。According to the results shown in FIG. 3, when the concentration of the suspended solids in the water to be treated is 50 ppm, the amount of water sampled per time is gradually increased in the case of this example as compared with the case of the comparative example. ,
It can be seen that the cleaning cycle is gradually increasing. In addition, when the concentration of the suspended substance becomes as high as 250 ppm, which is 5 times, in the comparative example, the rate of increase of the differential pressure also becomes 5 times, so that the amount of water taken per washing cycle is reduced to 1/5. On the other hand, in the present example, even if the concentration of the suspended substance was increased by 5 times,
The decrease in the amount of water taken per washing cycle can be suppressed to about 1/2. In other words, if the amount of water taken is the same, only one washing is required in this embodiment, but three washings are required in the comparative example, and the washing cycle is significantly lengthened.
【００３１】［濾過装置の概略仕様］ １．本実施例の濾過装置（図１に示す濾過装置） 密閉容器の高さ ：２.２ｍ 密閉容器の内径 ：０.１６ｍ 中空糸膜モジュールの本数：１本 中空糸膜モジュールの長さ：１.７ｍ 邪魔板の寸法 ：外径０.１４ｍ×内径０.１３
ｍ×高さ１.５ｍ ２．比較例の濾過装置（図４に示す濾過装置） 邪魔板を有さず、被処理水の流入配管位置を変更した以
外は本実施例の濾過装置に準じて構成されている。[General Specifications of Filtration Device] 1. Filtration device of this embodiment (filtration device shown in FIG. 1) Height of closed container: 2.2 m Inner diameter of closed container: 0.16 m Number of hollow fiber membrane modules: 1 Length of hollow fiber membrane module: 1. 7m Baffle Dimension: Outer Diameter 0.14m x Inner Diameter 0.13
m x height 1.5 m 2. Filtration Device of Comparative Example (Filtration Device Shown in FIG. 4) The filtration device of Comparative Example is configured without the baffle plate and the position of the inflow pipe of the water to be treated is changed.
【００３２】［被処理水の処理条件］ １．被処理水の懸濁物質の濃度：５０ｐｐｍ 通水流量 ：１.０ｍ3／ｈ ２．被処理水の懸濁物質の濃度：２５０ｐｐｍ 通水流量 ：１.０ｍ3／ｈ[Treatment Conditions for Treated Water] 1. Concentration of suspended solids in treated water: 50 ppm Flow rate: 1.0 m 3 / h 2. Concentration of suspended solids in treated water: 250 ppm Flow rate: 1.0 m 3 / h
【００３３】尚、本願発明は、被処理水が中空糸膜モジ
ュールへ到達する前に、下室内に流入する被処理水に旋
回流及び／または下降流を生起させて懸濁物質を被処理
水から沈降させる懸濁物質分離手段を下室に設けたもの
であれば良く、懸濁物質分離手段の具体的形態は上記各
実施形態に何等制限されるものではない。According to the present invention, before the water to be treated reaches the hollow fiber membrane module, a swirling flow and / or a downward flow is generated in the water to be treated flowing into the lower chamber to suspend the suspended matter. As long as the suspended substance separating means for sedimenting from the above is provided in the lower chamber, the specific form of the suspended substance separating means is not limited to the above embodiments.
【００３４】[0034]
【発明の効果】本発明の請求項１〜請求項３に記載の発
明によれば、懸濁物質の濃度が高い廃液が流入しても同
じ本数の中空糸膜モジュールでも１回当たりの採水量の
著しい減少と洗浄周期の著しい短縮を抑制することがで
きる中空糸膜濾過装置を提供することができる。According to the inventions of claims 1 to 3, even if a waste liquid having a high concentration of suspended substances flows in, the same amount of hollow fiber membrane modules can be used to collect water. It is possible to provide a hollow fiber membrane filtration device capable of suppressing a significant decrease in the cleaning cycle and a significant reduction in the cleaning cycle.
【図１】本発明の中空糸膜濾過装置の一実施形態の軸方
向断面を示す模式図である。FIG. 1 is a schematic view showing an axial cross section of an embodiment of a hollow fiber membrane filtration device of the present invention.
【図２】本発明の中空糸膜濾過装置の他の実施形態の軸
方向断面を示す模式図である。FIG. 2 is a schematic view showing an axial cross section of another embodiment of the hollow fiber membrane filtering device of the present invention.
【図３】図１に示す中空糸膜濾過装置の採水量と従来の
中空糸膜濾過装置の採水量とを比較したグラフである。FIG. 3 is a graph comparing the amount of water sampled by the hollow fiber membrane filtering device shown in FIG. 1 with the amount of water sampled by the conventional hollow fiber membrane filtering device.
【図４】従来の中空糸膜濾過装置の一例の軸方向断面を
示す模式図である。FIG. 4 is a schematic view showing an axial cross section of an example of a conventional hollow fiber membrane filtering device.
【図５】中空糸膜濾過装置に用いられる中空糸膜モジュ
ールを示す模式図である。FIG. 5 is a schematic view showing a hollow fiber membrane module used in a hollow fiber membrane filtration device.
１ 密閉容器 ２ 上室 ３ 下室 ４ 仕切板 ５ 中空糸膜モジュール ６ 流入配管（流入口） ７ 流出配管（流出口） １５ ガイド機構（懸濁物質分離手段） １５Ａ 邪魔板 １５Ｂ 邪魔板 １７ サイクロンセパレータ（懸濁物質分離手段） 1 Airtight container 2 Upper chamber 3 Lower chamber 4 Partition plate 5 Hollow fiber membrane module 6 Inflow pipe (inlet) 7 Outflow pipe (outlet) 15 Guide mechanism (suspended substance separating means) 15A Baffle plate 15B Baffle plate 17 Cyclone separator (Suspended substance separation means)
───────────────────────────────────────────────────── フロントページの続き (72)発明者 森田 利夫 埼玉県戸田市川岸１丁目４番９号 オルガ ノ株式会社総合研究所内 ─────────────────────────────────────────────────── ─── Continuation of front page (72) Inventor Toshio Morita 1-4-9 Kawagishi, Toda City, Saitama Organo Research Institute
Claims (3)
板と、この仕切板に上端が固定され且つ下端が下室へ垂
下する中空糸膜モジュールとを備え、上記下室に形成さ
れた流入口からこの室内に流入した被処理水を上記中空
糸膜モジュールを構成する多数本の中空糸膜によって濾
過して懸濁物質を除去し、その濾過水を上記上室に形成
された流出口から流出させる中空糸膜濾過装置におい
て、上記下室内に流入した被処理水を上記中空糸膜モジ
ュール下端と上記密閉容器の底部との間に設けた下部空
間に導くと共にその被処理水を上記中空糸膜モジュール
に流入させる前に旋回流及び／または下降流を生起させ
て懸濁物質を上記下部空間内に滞留させる懸濁物質分離
手段を上記下室に設けたことを特徴とする中空糸膜濾過
装置。1. A partition plate for partitioning the inside of an airtight container into an upper chamber and a lower chamber, and a hollow fiber membrane module having an upper end fixed to the partition plate and a lower end hanging down to the lower chamber, which is formed in the lower chamber. The water to be treated which has flowed into the chamber through the inflow port was filtered through a large number of hollow fiber membranes constituting the hollow fiber membrane module to remove suspended substances, and the filtered water was formed in the upper chamber. In the hollow fiber membrane filtering device that flows out from the outlet, the water to be treated that has flowed into the lower chamber is guided to the lower space provided between the lower end of the hollow fiber membrane module and the bottom of the closed container, and the water to be treated is introduced. The lower chamber is provided with a suspended substance separating means for causing a swirl flow and / or a downward flow to cause suspended substances to stay in the lower space before flowing into the hollow fiber membrane module. Fiber membrane filtration device.
内周面と上記中空糸膜モジュール群の間に設けられた筒
状の邪魔板と、この邪魔板の上端と上記下室内周面間の
隙間を塞ぐ邪魔板とを備えたことを特徴とする請求項１
に記載の中空糸膜濾過装置。2. A cylindrical baffle plate provided between the peripheral surface of the lower chamber and the hollow fiber membrane module group as the suspended substance separating means, and an upper end of the baffle plate and a peripheral surface of the lower chamber. 2. A baffle for closing the gap between the two is provided.
The hollow fiber membrane filtration device according to.
空間をサイクロンセパレータとして構成したことを特徴
とする請求項１に記載の中空糸膜濾過装置。3. The hollow fiber membrane filtering apparatus according to claim 1, wherein the lower space is configured as a cyclone separator as the suspended substance separating means.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP34562495A JP3282781B2 (en) | 1995-12-09 | 1995-12-09 | Hollow fiber membrane filtration device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP34562495A JP3282781B2 (en) | 1995-12-09 | 1995-12-09 | Hollow fiber membrane filtration device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH09155165A true JPH09155165A (en) | 1997-06-17 |
| JP3282781B2 JP3282781B2 (en) | 2002-05-20 |
Family
ID=18377868
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP34562495A Expired - Fee Related JP3282781B2 (en) | 1995-12-09 | 1995-12-09 | Hollow fiber membrane filtration device |
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| Country | Link |
|---|---|
| JP (1) | JP3282781B2 (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100403122B1 (en) * | 2001-02-01 | 2003-10-30 | 주식회사 대현하이테크 | Water cleaning device of a tank for sludge separation |
| JP2006159135A (en) * | 2004-12-09 | 2006-06-22 | Japan Organo Co Ltd | Hollow fiber membrane module |
-
1995
- 1995-12-09 JP JP34562495A patent/JP3282781B2/en not_active Expired - Fee Related
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100403122B1 (en) * | 2001-02-01 | 2003-10-30 | 주식회사 대현하이테크 | Water cleaning device of a tank for sludge separation |
| JP2006159135A (en) * | 2004-12-09 | 2006-06-22 | Japan Organo Co Ltd | Hollow fiber membrane module |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3282781B2 (en) | 2002-05-20 |
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