JPS6268599A - Apparatus for treating sewage - Google Patents
Apparatus for treating sewageInfo
- Publication number
- JPS6268599A JPS6268599A JP60205339A JP20533985A JPS6268599A JP S6268599 A JPS6268599 A JP S6268599A JP 60205339 A JP60205339 A JP 60205339A JP 20533985 A JP20533985 A JP 20533985A JP S6268599 A JPS6268599 A JP S6268599A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- tank
- aeration tank
- membrane
- separation means
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Aeration Devices For Treatment Of Activated Polluted Sludge (AREA)
Abstract
Description
【発明の詳細な説明】
(産業上の利用分野)
この発明は下水や、し尿を深層曝気槽で循環処理し、そ
の循環処理液の一部を限外濾過膜、精密濾過119等の
透過膜を内蔵した膜分離−L段を用いて除濁、除有機物
等の処理を行う汚水処理装置に関する。Detailed Description of the Invention (Field of Industrial Application) This invention circulates and processes sewage and human waste in a deep aeration tank, and transfers a portion of the circulating treatment liquid to a permeable membrane such as an ultrafiltration membrane or precision filtration 119. This invention relates to a sewage treatment device that performs turbidity removal, organic matter removal, and other treatments using a membrane separation L stage with a built-in membrane separation.
近年、処理施設用地の確保難、或は放流水質の高度化要
求のため、曝気処理した処理水を次に沈殿分離槽で処理
するのに代えて上述の様に膜処理することが研究、開発
されている。In recent years, due to the difficulty in securing land for treatment facilities and the demand for improved quality of effluent water, research and development has been carried out to perform membrane treatment as described above instead of treating aerated treated water in a sedimentation separation tank. has been done.
(従来の技術)
従来は特公昭4B−41584号公報に示されている様
に曝気槽での生物処理と、膜分離手段による処理は全く
別個のシステムとして組合わされていた。(Prior Art) Conventionally, as shown in Japanese Patent Publication No. 4B-41584, biological treatment in an aeration tank and treatment by membrane separation means have been combined as completely separate systems.
(発明が解決しようとする問題点)
このため運転時間の経過とともに進行する膜分離手段の
膜の汚染を定期的な薬品による洗n1で除去するので装
置全体の運転効率が低下する。(Problems to be Solved by the Invention) For this reason, the contamination of the membrane of the membrane separation means that progresses with the passage of operating time is removed by periodic cleaning with chemicals n1, which reduces the operating efficiency of the entire apparatus.
更に、膜分離一手段に供給する液の加圧は膜分離手段に
付属する循環ポンプに依存するので循環ポンプは大容量
のものを必要とし、設備費、ランニングコストがともに
嵩む。Furthermore, since pressurization of the liquid supplied to the membrane separation means depends on the circulation pump attached to the membrane separation means, the circulation pump needs to have a large capacity, which increases both equipment costs and running costs.
(問題点を解決するための手段)
そこで本発明は汚水処理装置として、槽内液を循環させ
るための循環系を有する深層曝気槽と。(Means for Solving the Problems) Accordingly, the present invention provides a sewage treatment apparatus including a deep aeration tank having a circulation system for circulating liquid in the tank.
」−記曝気槽の底部付近に設けられた限外濾過膜、精密
濾過膜等の透過膜を内蔵する膜分離手段と、前記循環系
を流れる液の一部を上記膜分離手段に供給するための供
給系と、前記脱会a+段のcla側の濃縮液を前記深層
曝気槽に返却する返却系と、前記膜分離−L段の透過側
の透過液を処理水として取り出すための取出系とを備え
たことを特徴とする。- Membrane separation means that incorporates a permeable membrane such as an ultrafiltration membrane or a precision filtration membrane provided near the bottom of the aeration tank, and for supplying a portion of the liquid flowing through the circulation system to the membrane separation means. a return system for returning the concentrate on the cla side of the desorption a+ stage to the deep aeration tank, and a take-out system for taking out the permeate on the permeate side of the membrane separation-L stage as treated water. It is characterized by having
(作 用)
曝気槽は種晶が約5〜数10mもある深層曝気槽で、膜
分離ト段はその底部付近に設けられている。そして、脱
会[=段への供給系は深層曝気槽の槽内液を循環させる
循環系から液の一部を脱会子sL段に供給するので、深
層曝気槽の水頭を脱会1F1段への加圧に有効に利用で
きる。そして、透過膜を透過して膜分離p段の透過側に
得られる処理水は取出系により後処理又は高度処理の装
置に供給し、膜分離手段のe線側の濃縮液は返却系で深
層曝気槽に返却し、深層曝気槽で循環処理する。(Function) The aeration tank is a deep aeration tank in which the seed crystals are about 5 to several tens of meters long, and the membrane separation stage is provided near the bottom of the tank. Since the supply system to the removal stage supplies part of the liquid from the circulation system that circulates the liquid in the deep aeration tank to the removal stage sL, the water head of the deep aeration tank is added to the removal stage 1F1 stage. It can be effectively used for pressure. The treated water that passes through the permeable membrane and is obtained on the permeate side of the membrane separation p stage is supplied to the after-treatment or advanced treatment equipment by the take-out system, and the concentrated liquid on the e-line side of the membrane separation means is sent to the deep layer in the return system. It is returned to the aeration tank and circulated in the deep aeration tank.
(実施例)
図示の各実施例において、1は前述した深層曝気槽、2
はその循環系、3は膜分離手段、3′はその限外濾過膜
、精密濾過IF2等の透過膜、3aは同じくそのC線側
、3bは透過側、4は上記循環系2を流れる液の一部を
L記脱会#手段の濃縮側に供給する供給系、6は上記膜
分離手段のe線側のe培液を深層曝気槽1に返却する返
却系、7は膜分離手段の透過膜3′を透過し、透過側3
bに得られる透過液を取出し、後処理又は高度処理の装
置に供給する取出系を示す。(Example) In each of the illustrated examples, 1 is the deep aeration tank described above, 2 is
3 is the circulation system, 3 is the membrane separation means, 3' is the permeation membrane such as the ultrafiltration membrane or microfiltration IF2, 3a is the C line side, 3b is the permeation side, and 4 is the liquid flowing through the circulation system 2. 6 is a return system that returns the e-culture solution on the e-line side of the membrane separation means to the deep aeration tank 1, and 7 is the permeation system of the membrane separation means. Transmits through the membrane 3', and the permeate side 3
b shows a take-off system for taking out the obtained permeate and supplying it to post-treatment or advanced treatment equipment.
深層曝気槽lは槽外上部に槽内の液が溢入する気液分離
槽8と、槽内中央に縦設され、底部に開口した降液管9
を備え、降液管9は上端部に空気吸引、混合用のインゼ
クタ10を有し、気液分離槽8の溢流堰8′よりも少し
下のレベルに曝気槽の槽壁を貫いて突入した原水の供給
管11が接続する。そして気液分離槽8の底は配管12
で循環ポンプ13の吸引側に連らなり、その吐出側は配
管14で前記インゼクタ10に連らなる。尚、15はイ
ンゼクタ10に空気を送入するブロア、1′は曝気槽l
、気液分#i槽8のト端を共通に塞ぐ上壁に設けたガス
抜き管である。The deep aeration tank l has a gas-liquid separation tank 8 into which the liquid inside the tank overflows into the upper part of the outside of the tank, and a downcomer pipe 9 that is installed vertically in the center of the tank and opens at the bottom.
The downcomer pipe 9 has an injector 10 for air suction and mixing at its upper end, and penetrates the tank wall of the aeration tank to a level slightly below the overflow weir 8' of the gas-liquid separation tank 8. A supply pipe 11 for raw water is connected. The bottom of the gas-liquid separation tank 8 is a pipe 12.
It is connected to the suction side of the circulation pump 13, and its discharge side is connected to the injector 10 through a pipe 14. In addition, 15 is a blower that sends air to the injector 10, and 1' is an aeration tank l.
This is a gas vent pipe provided on the upper wall that commonly closes the end of the gas/liquid #i tank 8.
これによって原水は供給管11から降液管9に供給され
て管9内を降下し、その際に後述する様に空気と混合し
て#素を溶解して管9丁端から槽内底部に出、L昇する
気泡で激しく攪拌されながら槽内断面一杯にL向流して
生物処理され、次いで気液分S槽8に溢入し、その底か
ら循環ポンプ13に行ってポンプでインゼクタ10に揚
液され、インゼクタ10を流ドする際にブロア15が送
気する空気を吸引して混合し、降液管9を降下し、循環
を行う。従って循環系2は図示の各実施例では降液管9
、深層曝気槽l、気液分S槽8、配管12)循環ポンプ
13、配管14、インゼクタ10で構成される。As a result, the raw water is supplied from the supply pipe 11 to the downcomer pipe 9 and descends inside the pipe 9. At this time, as will be described later, the raw water is mixed with air and dissolves the # element, which flows from the end of the pipe 9 to the bottom of the tank. While vigorously agitated by the rising air bubbles, the liquid flows countercurrently over the entire cross section of the tank for biological treatment, then overflows into the gas-liquid S tank 8, flows from the bottom to the circulation pump 13, and is pumped into the injector 10. When the liquid is pumped and flows through the injector 10, air blown by the blower 15 is sucked and mixed, and the liquid descends through the downcomer pipe 9 to perform circulation. The circulatory system 2 therefore includes a downcomer pipe 9 in each of the illustrated embodiments.
, deep aeration tank 1, gas-liquid separation S tank 8, piping 12) circulation pump 13, piping 14, and injector 10.
第1.2図の第1¥施例は膜分離手段3の複数を深層曝
気槽1の槽外底部の近傍に配置したのに対し、第3図の
第2実施例は複数の膜分離手段3を深層曝気槽1の底部
内に組込んだ点で相違するだけで、深層曝気槽と膜分離
手段の関係はまったく同じである。In the first embodiment shown in FIG. 1.2, a plurality of membrane separation means 3 are arranged near the outer bottom of the deep aeration tank 1, whereas in the second embodiment shown in FIG. The only difference is that 3 is incorporated into the bottom of the deep aeration tank 1, and the relationship between the deep aeration tank and the membrane separation means is exactly the same.
つまり、前記循環ポンプ13から吐出される液の一部は
供給系4によりサイクロン16に導き、こ−で遊動スラ
ッジや異物などを分離し返送汚泥として系外に排出し、
サイクロン18を出た液は次いでインゼクタ17に供給
され、こ−でブロア18、給気系5からの空気を吸引混
合したのち配管19で夫々の膜分離手段3・・・の濃縮
側3aに供給される。そして透過v3′を透過側3bに
出た透過液は取出系7により後処理ないし高度処理の装
置に供給し、透過膜3′を透過しないe培液はe線側3
aから返却系6で曝気槽1の底部内に返却する。That is, a part of the liquid discharged from the circulation pump 13 is guided to the cyclone 16 by the supply system 4, where floating sludge and foreign matter are separated and discharged out of the system as return sludge.
The liquid exiting the cyclone 18 is then supplied to the injector 17, where it sucks and mixes air from the blower 18 and the air supply system 5, and then is supplied to the concentration side 3a of each membrane separation means 3 through a pipe 19. be done. Then, the permeate v3' that has come out on the permeate side 3b is supplied to a post-processing or advanced treatment device by the take-out system 7, and the e-culture liquid that does not pass through the permeable membrane 3' is on the e-line side 3.
A is returned to the bottom of the aeration tank 1 through a return system 6.
尚、第1実施例では脱会子aL段3は曝気槽の外に配置
されているので返却系6は槽内底部に突入する配管であ
り、この配管は第2図に示した様に濃縮液を接線方向に
入れ、槽内での混合攪拌を良好に行わせる様にするとよ
い。In the first embodiment, since the degassing element aL stage 3 is placed outside the aeration tank, the return system 6 is a pipe that enters the bottom of the tank, and this pipe is used to collect the concentrated liquid as shown in Fig. 2. It is preferable to add the liquid in the tangential direction to ensure good mixing and agitation in the tank.
又、第2実施例では各膜分離・1段3は曝気槽lの底部
内に組込んであるため返却系6には特に配管は必要でな
く、孔でもよい。Further, in the second embodiment, since each membrane separation/first stage 3 is built into the bottom of the aeration tank 1, no particular piping is required for the return system 6, and a hole may be used instead.
この様に膜分離手段3の透過膜3′を透過させるに必要
なe縮側3aへの液の加圧は深層曝気槽1の水頭圧が利
用できるのでyfI環ボンズ13の吐出圧は小さくても
よい。そして、給気系5により空気を混合した液をC線
側に供給するための透過膜3′は気泡のバブリング攪拌
により揺動し、巾に液だけを供給する場合と比較して数
倍の攪拌効果があり、膜に付着した汚染物質を剥離する
と共に、膜への汚染物質の付着を防止し、これにより膜
洗浄の実施回数を減少して施設の稼動率を高め、又、洗
浄に必要な薬品、労力を少なくし、施設の経済性を高め
ることができる。In this way, the water head pressure of the deep aeration tank 1 can be used to pressurize the liquid to the e-contraction side 3a necessary for permeating the permeable membrane 3' of the membrane separation means 3, so the discharge pressure of the yfI ring bond 13 is small. Good too. The permeable membrane 3' for supplying the liquid mixed with air to the C line side by the air supply system 5 is oscillated by the bubbling agitation of air bubbles, and the width is several times larger than when only the liquid is supplied. It has an agitating effect and removes contaminants that have adhered to the membrane, and also prevents contaminants from adhering to the membrane.This reduces the number of times membrane cleaning is performed and increases the operating rate of the facility. The cost of chemicals and labor can be reduced, making the facility more economical.
尚、第2実施例には図示を省略したが、複数の膜分離手
段3・・・は個別に定期的に点検、洗浄を行える様に弁
v1、Vl’で供給系4や曝気槽1から切)し3薬品洗
?′/I槽19の洗浄水を循環ポンプで個々の膜分離P
段のe線側に送入して薬品洗浄槽に循環させる様にする
。Although not shown in the second embodiment, the plurality of membrane separation means 3... are connected to the supply system 4 and the aeration tank 1 by valves v1 and Vl' so that they can be inspected and cleaned individually and regularly. Cut) 3 Chemical washing? ' / I tank 19 wash water is separated into individual membranes P using a circulation pump.
It is fed into the e-line side of the stage and circulated to the chemical cleaning tank.
又、循環系2を流れる液を膜分離り段3に供給する埴は
曝気槽1での滞流時間により適宜調節するものとし、そ
のためには循環ポンプ13がインゼクタ10に揚液する
配管14の途中と、供給系4の人「1に流量調節ブr2
0.21を1没けて置く。In addition, the flow rate for supplying the liquid flowing through the circulation system 2 to the membrane separation stage 3 shall be appropriately adjusted by the residence time in the aeration tank 1. On the way, supply system 4 person ``1 to flow rate adjustment brake r2
Place 0.21 one submersion.
第4図の実施例は第1.2図の実施例とは(同じであり
、同じ部分には回し符号を付して説IIを省略する。こ
の実施例が第1実施例と相違する主な点は気液分#槽8
の底から循環ポンプ13に循環液を導く配管12の途中
に供給系4を接続し、この供給系4の途中に膜分離手段
3・・・への送液ポンプ22を接続し、サイクロン!6
、インゼクタ17を経て119分離手段3・・・に送液
する様にした点である。The embodiment shown in FIG. 4 is the same as the embodiment shown in FIGS. The point is gas-liquid #tank 8
A supply system 4 is connected to the middle of the pipe 12 that leads the circulating liquid from the bottom of the cyclone to the circulation pump 13, and a liquid feeding pump 22 to the membrane separation means 3 is connected to the middle of this supply system 4. 6
, the liquid is sent to the separation means 3 119 through the injector 17.
この実施例は深層曝気槽1の検品が比較的低く、膜分離
手段3の透過膜に加える有効圧力が水頭で充分に得られ
ないとき、これを送液ポンプ22の吐出圧で補うのであ
る。In this embodiment, when the inspection quality of the deep aeration tank 1 is relatively low and the effective pressure applied to the permeable membrane of the membrane separation means 3 cannot be sufficiently obtained from the water head, this is compensated for by the discharge pressure of the liquid feed pump 22.
勿論、この実施例も前述の第1、第2実施例と同様に機
俺する。Of course, this embodiment also operates in the same manner as the first and second embodiments described above.
(発明の効果)
本発明によれば膜分離手段の膜汚染の進行を常に防止し
ながら運転が継続でき、装置の稼動率が高い。又、深層
曝気槽との組合せによりその水頭を膜分離手段への有効
圧力として利用するので循環ポンプの動力の低減が図れ
る。更に膜分離手段内の加圧下で液と空気が透過膜を攪
拌すると共に、混合し、空気の液への溶解を促進する。(Effects of the Invention) According to the present invention, operation can be continued while constantly preventing the progress of membrane contamination of the membrane separation means, and the operating rate of the apparatus is high. Furthermore, in combination with a deep aeration tank, the water head is used as effective pressure for the membrane separation means, so the power of the circulation pump can be reduced. Furthermore, under pressure within the membrane separation means, the liquid and air agitate and mix with the permeable membrane, promoting dissolution of the air into the liquid.
第1図は本発明の第1実施例の系統図、第2図はLの要
部のモ面配置図、第3図は本発明の第2実施例の系統図
、第4図は本発明の更に他の一実施例の系統図で、図中
、1は深層曝気槽、2はその循環系、3は膜分離手段、
3′はその透過膜、3aはそのC線側、3bは同じく透
過側。
4は膜分離手段への供給系、6は返却系、7は取出系を
示す。
第2fI!Fig. 1 is a system diagram of the first embodiment of the present invention, Fig. 2 is a cross-sectional layout diagram of the main parts of L, Fig. 3 is a system diagram of the second embodiment of the invention, and Fig. 4 is the system diagram of the present invention. In the diagram, 1 is a deep aeration tank, 2 is its circulation system, 3 is a membrane separation means,
3' is its transmission membrane, 3a is its C line side, and 3b is its transmission side. 4 is a supply system to the membrane separation means, 6 is a return system, and 7 is a take-out system. 2nd fI!
Claims (2)
気槽と、上記曝気槽の底部付近に設けられた限外濾過膜
、精密濾過膜等の透過膜を内蔵する膜分離手段と、前記
循環系を流れる液の一部を上記膜分離手段に供給するた
めの供給系と、前記膜分離手段の濃縮側の濃縮液を前記
深層曝気槽に返却する返却系と、前記膜分離手段の透過
側の透過液を処理水として取り出すための取出系とを備
えたことを特徴とする汚水処理装置。(1) A deep aeration tank having a circulation system for circulating the liquid in the tank, and a membrane separation means having a built-in permeable membrane such as an ultrafiltration membrane or a microfiltration membrane provided near the bottom of the aeration tank; a supply system for supplying a part of the liquid flowing through the circulation system to the membrane separation means; a return system for returning the concentrated liquid on the concentration side of the membrane separation means to the deep aeration tank; A sewage treatment device comprising: a take-out system for taking out permeate on the permeate side as treated water.
前記膜分離手段への供給系には固液分離手段が設けられ
ている汚水処理装置。(2) In the sewage treatment device according to claim (1),
A wastewater treatment apparatus, wherein a supply system to the membrane separation means is provided with a solid-liquid separation means.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60205339A JPS6268599A (en) | 1985-09-19 | 1985-09-19 | Apparatus for treating sewage |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP60205339A JPS6268599A (en) | 1985-09-19 | 1985-09-19 | Apparatus for treating sewage |
Publications (1)
Publication Number | Publication Date |
---|---|
JPS6268599A true JPS6268599A (en) | 1987-03-28 |
Family
ID=16505267
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP60205339A Pending JPS6268599A (en) | 1985-09-19 | 1985-09-19 | Apparatus for treating sewage |
Country Status (1)
Country | Link |
---|---|
JP (1) | JPS6268599A (en) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH02194894A (en) * | 1989-01-25 | 1990-08-01 | D Bii S Kk | Sewage treatment apparatus |
JP2013240794A (en) * | 2008-11-11 | 2013-12-05 | Kobelco Eco-Solutions Co Ltd | Membrane separation activated sludge treatment apparatus, and membrane separation activated sludge treatment method |
-
1985
- 1985-09-19 JP JP60205339A patent/JPS6268599A/en active Pending
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPH02194894A (en) * | 1989-01-25 | 1990-08-01 | D Bii S Kk | Sewage treatment apparatus |
JPH0683831B2 (en) * | 1989-01-25 | 1994-10-26 | デイビイエス株式会社 | Sewage treatment method |
JP2013240794A (en) * | 2008-11-11 | 2013-12-05 | Kobelco Eco-Solutions Co Ltd | Membrane separation activated sludge treatment apparatus, and membrane separation activated sludge treatment method |
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