JP3106066B2 - Septic tank - Google Patents
Septic tankInfo
- Publication number
- JP3106066B2 JP3106066B2 JP24613194A JP24613194A JP3106066B2 JP 3106066 B2 JP3106066 B2 JP 3106066B2 JP 24613194 A JP24613194 A JP 24613194A JP 24613194 A JP24613194 A JP 24613194A JP 3106066 B2 JP3106066 B2 JP 3106066B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- water
- membrane separation
- treated
- return
- 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.)
- Expired - Fee Related
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)
- Treatment Of Biological Wastes In General (AREA)
- Activated Sludge Processes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
【0001】[0001]
【産業上の利用分野】本発明は、嫌気処理槽と、膜分離
槽とを備え、前記嫌気処理槽と、膜分離槽との間に、嫌
気処理槽を経た被処理水を受ける中間処理槽を設けてあ
る浄化槽に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention comprises an anaerobic treatment tank and a membrane separation tank, and an intermediate treatment tank between the anaerobic treatment tank and the membrane separation tank for receiving water to be treated that has passed through the anaerobic treatment tank. The present invention relates to a septic tank provided with:
【0002】[0002]
【従来の技術】この種の浄化槽は、膜分離槽で被処理水
を固液分離処理するために、長期にわたって運転を続け
ると、前記膜分離槽において被処理水中の汚泥等の濃度
が高くなってくることがある。ところが、膜分離槽内で
汚泥等の固形成分濃度が異常に高くなった場合には、前
記膜分離槽内の膜分離装置が、目詰まりし易くなるた
め、長期にわたって浄化槽を効率よく運転するために
は、前記膜分離槽内の固形成分濃度が高くなりすぎない
ようにして、前記膜分離装置による膜分離処理を行う環
境を良好に維持させる必要性があると考えられていた。2. Description of the Related Art If this type of septic tank is operated for a long period of time in order to subject the water to be treated to solid-liquid separation in a membrane separation tank, the concentration of sludge and the like in the water to be treated increases in the membrane separation tank. May come. However, when the concentration of solid components such as sludge in the membrane separation tank becomes abnormally high, the membrane separation device in the membrane separation tank is easily clogged, so that the purification tank is efficiently operated for a long period of time. It has been considered that it is necessary to prevent the solid component concentration in the membrane separation tank from becoming too high in order to maintain a favorable environment for performing the membrane separation treatment by the membrane separation apparatus.
【0003】そのため、上述の目的を達成するために、
膜分離槽内の汚泥成分を含む被処理水をエアリフトポン
プを用いて嫌気処理槽に返送して、前記汚泥成分を嫌気
処理させ、前記膜分離槽内の固形成分濃度が高くなりす
ぎないように調節することが考えられていた。[0003] Therefore, in order to achieve the above object,
The treated water containing the sludge component in the membrane separation tank is returned to the anaerobic treatment tank using an air lift pump, and the sludge component is subjected to anaerobic treatment so that the solid component concentration in the membrane separation tank does not become too high. It was supposed to adjust.
【0004】[0004]
【発明が解決しようとする課題】ところが、エアリフト
ポンプで被処理水を常時、嫌気処理槽に返送している
と、膜分離槽内の汚泥濃度が低くなりすぎるとともに、
前記嫌気処理槽の被処理水が好気状態に近づきぎみに変
化してしまうなどの不都合が考えられるため、前記被処
理水の返送は常時行うわけにもゆかず、制御装置を用い
て間欠的に行わねばならないと考えられる。However, if the water to be treated is constantly returned to the anaerobic treatment tank by the air lift pump, the sludge concentration in the membrane separation tank becomes too low,
Due to the inconvenience that the water to be treated in the anaerobic treatment tank approaches the aerobic state and changes suddenly, the return of the water to be treated cannot be always performed, and is intermittently performed using a control device. It must be done in
【0005】このような状況にあって、エアリフトポン
プによる被処理水の返送を行うには、前記制御装置や、
前記エアリフトポンプに空気供給するブロワを設けるな
ど、装置として複雑にならざるを得ず、また、複雑で高
価な装置を設けるが故に高価にならざるを得なかった。In such a situation, the return of the water to be treated by the air lift pump requires the control device
The apparatus must be complicated, such as providing a blower for supplying air to the air lift pump, and the apparatus must be expensive due to the provision of a complicated and expensive apparatus.
【0006】従って、本発明の目的は、上記実情に鑑
み、簡単な構成で、安価に膜分離槽内の汚泥成分を含む
被処理水を嫌気処理槽に返送して、その中の前記汚泥成
分を嫌気処理させ、前記膜分離槽内の固形成分濃度が高
くなりすぎないように調節できる浄化槽を提供すること
にある。SUMMARY OF THE INVENTION Accordingly, an object of the present invention is to provide a simple structure and inexpensively return the water to be treated containing the sludge component in the membrane separation tank to the anaerobic treatment tank with the simple configuration in view of the above situation. And an anaerobic treatment of the water, and to provide a purification tank capable of adjusting the solid component concentration in the membrane separation tank so as not to be too high.
【0007】[0007]
【課題を解決するための手段】この目的を達成するため
の本発明の特徴構成は、膜分離槽に被処理水を移送する
移送ポンプを前記中間処理槽に設け、前記膜分離槽の被
処理水を、オーバーフローで前記中間処理槽へ返送する
第一返送路、及び、前記膜分離槽の被処理水を、オーバ
ーフローで前記嫌気処理槽へ返送する第二返送路を設
け、前記第一返送路を介して前記中間処理槽へ返送され
る被処理水が設定量を超過したときに、その設定量を超
過する被処理水を前記第二返送路を介して前記嫌気処理
槽へ返送するための流量設定部を設けたことにあり、前
記膜分離槽の隔壁に被処理水の返送部を設け、前記返送
部と前記嫌気処理槽とにわたって返送管を架設し、その
返送管の一端を前記返送部に接続して、前記返送管にお
ける前記返送部から前記返送管の他端までの部分に第二
返送路を形成するとともに、前記返送管の中間部で前記
中間処理槽上方に被処理水を落下させる落下口を形成し
て流量設定部を構成し、かつ、前記返送管における前記
返送部から前記落下口までの部分に第一返送路を形成し
てあってもよく、前記流量設定部に第一返送路に流れる
被処理水の最大流量を設定する堰を設けてあってもよ
く、その作用効果は以下の通りである。In order to achieve this object, a feature of the present invention is to provide a transfer pump for transferring water to be treated to a membrane separation tank in the intermediate treatment tank, A first return path for returning water to the intermediate treatment tank by overflow, and a second return path for returning water to be treated in the membrane separation tank to the anaerobic treatment tank by overflow, wherein the first return path When the water to be treated returned to the intermediate treatment tank through the set amount exceeds the set amount, the water to be treated exceeding the set amount is returned to the anaerobic treatment tank through the second return path. Because of the provision of the flow rate setting section, a return section for the water to be treated is provided on the partition wall of the membrane separation tank, a return pipe is laid across the return section and the anaerobic treatment tank, and one end of the return pipe is returned to the membrane. Section, from the return section in the return pipe A second return path is formed in the portion up to the other end of the return pipe, and a drop port for dropping the water to be treated is formed above the intermediate treatment tank at an intermediate portion of the return pipe to constitute a flow rate setting section. And, a first return path may be formed in a portion from the return section to the drop port in the return pipe, and the maximum flow rate of the water to be treated flowing through the first return path is set in the flow rate setting section. A weir may be provided, and its operation and effect are as follows.
【0008】[0008]
【作用】つまり、請求項1記載の構成によれば、通常被
処理水は、移送ポンプにより、被処理水が膜分離槽に移
送され、さらに、オーバーフローにより前記第一返送路
を介して前記中間処理槽に返送される循環を繰り返し、
このとき、移送ポンプの被処理水返送量と、前記第一返
送路を介して返送される被処理水と膜分離されて膜分離
槽外に排出される被処理水の和とのバランスが保たれ
る。In other words, according to the structure of the first aspect, the water to be treated is usually transferred to the membrane separation tank by a transfer pump, and furthermore, overflowed through the first return path to the intermediate water. Repeat the circulation returned to the processing tank,
At this time, the balance between the amount of the water to be treated returned by the transfer pump and the sum of the water to be treated returned through the first return path and the water to be treated separated into a membrane and discharged to the outside of the membrane separation tank is maintained. Dripping.
【0009】ところが、膜分離槽内で、MLSSが過剰
に増大し、膜分離による透過水量が低下すると、前記バ
ランスが崩れ、次第に膜分離槽内の水位が上昇する。そ
のため、前記第一返送路からオーバーフローで返送され
る被処理水量が増加する。この被処理水量が前記流量設
定部で設定される設定量を超過するとその超過した被処
理水は、第二返送路を介して前記嫌気処理槽へ返送され
る。However, if the MLSS increases excessively in the membrane separation tank and the amount of permeated water decreases due to membrane separation, the above-mentioned balance is lost, and the water level in the membrane separation tank gradually rises. Therefore, the amount of water to be treated returned from the first return path by overflow increases. When the amount of water to be treated exceeds the set amount set by the flow rate setting section, the excess water to be treated is returned to the anaerobic treatment tank via the second return path.
【0010】[0010]
【発明の効果】その結果、前記膜分離槽内の汚泥成分
は、嫌気処理槽内で嫌気処理されるとともに、嫌気処理
槽から汚泥成分の少ない被処理水が中間処理槽を経て前
記膜分離槽に供給されることになるから、前記膜分離槽
内の汚泥濃度は低下する。前記汚泥濃度が低下すると前
記膜分離槽において膜分離装置が、目詰まりしにくくな
るので、前記膜分離装置の膜面が前記膜分離槽内の被処
理水の流れ等によって洗浄される効果が大となり、前記
膜分離装置の目詰まりは解消されやすい。そのため、前
記膜分離装置の膜分離性能が回復し、前記被処理水の循
環するバランスが回復するとともに、前記膜分離槽内の
水位が通常の位置にまで低下し、前記膜分離槽は、再び
安定した膜分離処理を行えることになる。As a result, the sludge component in the membrane separation tank is subjected to anaerobic treatment in the anaerobic treatment tank, and water to be treated having a small amount of sludge component is removed from the anaerobic treatment tank through the intermediate treatment tank. , The sludge concentration in the membrane separation tank decreases. When the sludge concentration is reduced, the membrane separation device in the membrane separation tank is less likely to be clogged. Therefore, the effect of cleaning the membrane surface of the membrane separation device by the flow of the water to be treated in the membrane separation tank is large. Thus, clogging of the membrane separation device is easily eliminated. Therefore, the membrane separation performance of the membrane separation device is restored, the balance of the circulating water is restored, and the water level in the membrane separation tank is reduced to a normal position, and the membrane separation tank is again A stable membrane separation process can be performed.
【0011】従って、被処理水の返送ポンプなどの特別
な構成を要しない簡単な構成をもって、被処理水を前記
膜分離槽と前記嫌気処理槽とのあいだで循環させるだけ
で、前記膜分離槽内において汚泥等の固形成分濃度が高
くなりすぎるような不都合を解消することが出来たか
ら、前記膜分離槽の膜分離性能は安定して高く維持でき
るようになった。[0011] Therefore, the membrane separation tank can be simply circulated between the membrane separation tank and the anaerobic treatment tank by a simple configuration that does not require a special configuration such as a return pump for the water. The inconvenience that the solid component concentration of sludge or the like becomes too high in the inside can be eliminated, so that the membrane separation performance of the membrane separation tank can be stably maintained at a high level.
【0012】また、請求項2記載の構成によれば、返送
管をもって、第一、第二返送路を構成するとともに、落
下口をもって、流量設定部を構成することが出来るの
で、尚一層簡単な構成で上記作用を実現できるととも
に、請求項3記載の構成によれば、流量設定部に堰を設
けてあるから、被処理水が設定流量以下の場合にその被
処理水を確実に第一返送路に導くことが出来る。Further, according to the second aspect of the present invention, the first and second return paths can be constituted by the return pipe, and the flow rate setting section can be constituted by the drop port. According to the third aspect of the present invention, since the weir is provided in the flow rate setting unit, when the water to be treated is equal to or less than the set flow rate, the water to be treated is surely returned to the first position. You can lead to the road.
【0013】[0013]
【実施例】以下に本発明の浄化槽を図面に基づいて説明
する。図1に示すように、上流側から順に、沈殿分離槽
N1、嫌気瀘床槽N2、脱窒槽E1、膜分離槽E2、消
毒槽Q、貯留槽Tを被処理水が移流するように設けて浄
化槽を構成してある。DESCRIPTION OF THE PREFERRED EMBODIMENTS A septic tank according to the present invention will be described below with reference to the drawings. As shown in FIG. 1, a sedimentation separation tank N1, an anaerobic filtration tank N2, a denitrification tank E1, a membrane separation tank E2, a disinfection tank Q, and a storage tank T are provided in order from the upstream side so that the water to be treated flows. A septic tank is configured.
【0014】前記沈殿分離槽N1は、流入口Iから浄化
槽内に流入した被処理水の原水を受けて、その被処理水
中の夾雑物を沈澱除去しつつ、内部に生育する嫌気性菌
により、被処理水を嫌気処理し、嫌気瀘床槽N2に移流
自在に構成してある。The sedimentation separation tank N1 receives raw water to be treated which has flowed into the septic tank from the inlet I, and precipitates and removes contaminants in the water to be treated. The water to be treated is anaerobically treated and is configured to be freely transferred to the anaerobic filter bed tank N2.
【0015】前記嫌気瀘床槽N2は、流入した被処理水
を嫌気処理する嫌気性菌を育成しうる嫌気瀘床Fを内装
してあり、前記沈殿分離槽N1から移流してきた被処理
水を嫌気処理して前記膜分離槽E2に移流するように構
成してある。The anaerobic filter tank N2 is provided with an anaerobic filter F capable of growing anaerobic bacteria for anaerobically treating the inflowing water to be treated. The anaerobic treatment is performed and the water is transferred to the membrane separation tank E2.
【0016】前記脱窒槽E1は、前記嫌気瀘床槽N2か
ら流入した比較的固形成分濃度の低い被処理水を一次貯
留しつつ、被処理水を主に脱窒処理する脱窒菌を内部に
育成する構成にしてある。また、前記脱窒槽E1にはエ
アリフト作用で被処理水を汲み上げて膜分離槽E2に移
送させる移送ポンプAを内装してあり、定常的に被処理
水を膜分離槽E2に移送する構成にしてある。The denitrification tank E1 is for temporarily storing the water to be treated having a relatively low solid component concentration and flowing from the anaerobic filter bed tank N2, and growing therein denitrifying bacteria for mainly denitrifying the water to be treated. Configuration. Further, the denitrification tank E1 is equipped with a transfer pump A for pumping up the water to be treated by an air lift function and transferring it to the membrane separation tank E2, and is configured to constantly transfer the water to be treated to the membrane separation tank E2. is there.
【0017】前記膜分離槽E2は、多数の平膜を並設し
てなる膜分離装置Mを内装してなり、その膜分離装置M
の下方には、その膜分離装置Mに気泡を供給して、その
膜面に汚泥等の付着しすぎるのを防止し、かつ、前記膜
分離槽E2内に循環流を形成しながら被処理水に酸素を
供給する散気装置Dを内装し、また、前記膜分離装置M
のそれぞれの平膜には集水管M1を連設し、前記膜分離
槽E2の水面よりも下方で前記膜分離槽E2に隣接して
設けてある消毒槽Qに連通接続してある。The membrane separation tank E2 is provided with a membrane separation device M in which a number of flat membranes are arranged in parallel.
Bubble is supplied to the membrane separation device M to prevent sludge from adhering excessively to the membrane surface, and the water to be treated is formed while forming a circulating flow in the membrane separation tank E2. And an air diffuser D for supplying oxygen to the membrane.
A water collecting pipe M1 is connected to each of the flat membranes, and is connected to a disinfection tank Q provided below and adjacent to the membrane separation tank E2 below the water surface of the membrane separation tank E2.
【0018】また、前記膜分離槽E2と、前記脱窒槽E
1とを仕切る隔壁Eeに被処理水返送口1を設けるとと
もに、その被処理水返送口1と前記沈殿分離槽N1との
あいだにわたって架設してある返送管2の基端部2aを
連通接続してある。Further, the membrane separation tank E2 and the denitrification tank E
1 and a base end portion 2a of a return pipe 2 extending between the treated water return port 1 and the sedimentation separation tank N1. It is.
【0019】前記返送管2は、前記被処理水返送口1と
前記沈殿分離槽N1との間にわたって架設してあり、図
2に示すように、その返送管2には、前記脱窒槽E1上
方の中間部において、落下口3を設けてあり、前記被処
理水返送口1と、前記落下口3とのあいだの部分に、前
記膜分離槽E2内の被処理水を前記脱窒槽E1に返送す
る第一返送路21を形成してあるとともに、前記被処理
水返送口1と、前記返送管2の先端部2bとのあいだの
部分に、前記膜分離槽E2内の被処理水を前記沈殿分離
槽N1に返送する第二返送路22を形成してある。ま
た、前記返送管2の前記落下口3よりも先端部2b側に
は、前記返送管2の軸心回りで回動・固定自在な回動部
4を設け、その回動部4内には断面視で内部流路の略2
分の1を覆う堰4aを設けてある。尚、前記回動部4
は、前記堰4aが流路の下半分を覆うように固定されて
いるものである(図2(ロ)参照)。The return pipe 2 extends between the treated water return port 1 and the sedimentation separation tank N1. As shown in FIG. 2, the return pipe 2 is provided above the denitrification tank E1. A drop port 3 is provided at an intermediate portion of the tank, and the water to be treated in the membrane separation tank E2 is returned to the denitrification tank E1 at a portion between the treated water return port 1 and the fall port 3. A first return path 21 is formed, and the water to be treated in the membrane separation tank E2 is set in the portion between the treated water return port 1 and the tip 2b of the return pipe 2. A second return path 22 for returning to the separation tank N1 is formed. Further, a rotating portion 4 that is rotatable and fixable around the axis of the return tube 2 is provided on the tip 2 b side of the return port 2 with respect to the drop port 3. Approximately 2 of internal flow path in cross section
A weir 4a covering one half is provided. The rotating part 4
In FIG. 2, the weir 4a is fixed so as to cover the lower half of the flow path (see FIG. 2B).
【0020】その結果、前記膜分離槽E2内の被処理水
は、前記膜分離槽E2の水面と、前記集水管の前記消毒
槽Q側開口との水頭差によって、前記平膜で濾過され、
濾過済の処理水は、前記集水管M1を通じて消毒槽Qに
移流する。また、前記移送ポンプから流入した被処理水
は、前記返送管2により、通常は、第一返送路21を経
て前記落下口3から前記脱窒槽E1へ全量返送され、膜
分離槽E2内の水位が上昇したときには、前記返送管2
に流入する被処理水のうち、前記堰4aを越えないもの
については前記第一返送路21を経て前記落下口3から
前記脱窒槽E1へ返送され、前記堰4aを越えたものに
ついては、前記第二返送路22を経て前記返送管2先端
部22開口から前記沈殿分離槽N1に返送される構成と
なっている。As a result, the water to be treated in the membrane separation tank E2 is filtered by the flat membrane due to the head difference between the water surface of the membrane separation tank E2 and the opening of the water collection pipe on the disinfection tank Q side.
The filtered treated water is transferred to the disinfection tank Q through the water collecting pipe M1. Normally, all the water to be treated flowing from the transfer pump is returned to the denitrification tank E1 from the dropping port 3 through the return pipe 2 through the first return path 21, and the water level in the membrane separation tank E2 is returned. Rises, the return pipe 2
Of the water to be treated flowing into the denitrification tank E1 through the first return path 21, the water that does not exceed the weir 4a is returned to the denitrification tank E1. It is configured to be returned to the sedimentation / separation tank N1 from the opening of the end portion 22 of the return pipe 2 via the second return path 22.
【0021】つまり、例えば、前記移送ポンプAの被処
理水移送能力を5リットル/分に設定し、前記膜分離装
置Mの濾過能力が通常1リットル/分である場合を考え
れば、前記落下口3から前記脱窒槽E1に返送される被
処理水量を最大4リットル/分に設定しておくことで、
被処理水は、第一返送路21を経て前記落下口3から前
記脱窒槽E1へ全量返送され、定常的な膜分離処理が行
える。この状態で前記膜分離装置Mの濾過能力が0.8
リットル/分にまで低下したとすると、前記膜分離槽E
2に流入する被処理水は0.2リットル/分の割合で過
剰になるので、前記膜分離槽E2の水面は上昇し、前記
返送管2に流入する被処理水は前記堰4aを越え、前記
0.2リットル/分の被処理水が、前記沈殿分離槽N1
に返送されることになる。前記沈殿分離槽N1に被処理
水の返送があれば、浄化槽内への原水流入の有無に係わ
らず、嫌気処理されて固形分の少なくなった被処理水
が、前記脱窒槽E1に流入し、前記脱窒槽E1内の固形
分濃度を低下させるとともに、前記脱窒槽E1内の被処
理水が流入する前記膜分離槽E2内においても固形分濃
度が低下する。その結果、前記膜分離槽E2内の固形分
濃度の低下を受けて前記散気装置Dによる散気作用等に
よる前記膜分離装置Mの洗浄作用が向上し、前記膜分離
装置Mの濾過能力が1リットル/分まで回復し、定常的
な膜分離処理が再開出来るようになる。尚、このような
構成によれば、定常運転時には、前記膜分離槽E2内の
水位は一定に保たれるので、前記膜分離装置Mの被処理
水濾過圧は一定に保て、膜分離済の処理水は定常的に消
毒槽Qに移送され、消毒槽Qに移流する処理水の量を管
理するだけで前記膜分離槽E2の目詰まりの状況を把握
しやすいという利点もある。また、前記堰4aは、回動
させることで、前記第一返送路21に流れる被処理水の
最大流量を変更可能であるから、膜分離装置Mの性能に
よって被処理水の返送流量を設定変更できる利点があ
る。That is, for example, when the transfer capacity of the transfer pump A is set to 5 liters / minute and the filtration capacity of the membrane separation device M is usually 1 liter / minute, By setting the amount of water to be treated returned from 3 to the denitrification tank E1 at a maximum of 4 liters / minute,
The entire amount of the water to be treated is returned from the falling port 3 to the denitrification tank E1 via the first return path 21, so that a steady membrane separation process can be performed. In this state, the filtration capacity of the membrane separation device M is 0.8
Liter / minute, the membrane separation tank E
2 is excessive at a rate of 0.2 liter / minute, the water level of the membrane separation tank E2 rises, and the water flowing into the return pipe 2 passes over the weir 4a, The water to be treated at a rate of 0.2 liter / min.
Will be returned to If the water to be treated is returned to the sedimentation separation tank N1, the water to be treated that has been subjected to the anaerobic treatment and has a reduced solid content flows into the denitrification tank E1, regardless of whether raw water flows into the septic tank, The solids concentration in the denitrification tank E1 is reduced, and the solids concentration is also reduced in the membrane separation tank E2 into which the water to be treated in the denitrification tank E1 flows. As a result, in response to a decrease in the solid concentration in the membrane separation tank E2, the washing action of the membrane separation apparatus M by the air diffusion action by the air diffusion apparatus D is improved, and the filtration capacity of the membrane separation apparatus M is reduced. It recovers to 1 liter / min, and the regular membrane separation process can be resumed. According to such a configuration, during steady operation, the water level in the membrane separation tank E2 is kept constant, so that the filtration pressure of the water to be treated in the membrane separation device M is kept constant, and the membrane separation is completed. This treatment water is constantly transferred to the disinfection tank Q, and there is an advantage that the clogging state of the membrane separation tank E2 can be easily grasped only by controlling the amount of the treatment water flowing to the disinfection tank Q. Further, since the maximum flow rate of the water to be treated flowing through the first return path 21 can be changed by rotating the weir 4a, the return flow rate of the water to be treated is changed according to the performance of the membrane separation device M. There are advantages that can be done.
【0022】前記消毒槽Qに流入した被処理水は、消毒
されたのち貯留槽Tで貯留され、吸引ポンプPで汲み上
げられ、放流口Zから浄化槽外へ放流される構成にして
ある。The water to be treated, which has flowed into the disinfecting tank Q, is stored in a storage tank T after being disinfected, pumped up by a suction pump P, and discharged from a discharge port Z to the outside of the purification tank.
【0023】〔別実施例〕先の実施例では、浄化槽を、
流入口I側から順に沈殿分離槽N1、嫌気濾床槽N2、
脱窒槽E1、膜分離槽E2を設けて構成したが、これに
限らず、例えば、前記嫌気濾床槽N2に替えて、被処理
水を好気処理する好気性菌を育成する好気濾床を内装し
てなる好気濾床槽を設けて浄化槽を構成してあってもよ
く、要するに、嫌気処理槽と、膜分離槽E2を備えてな
る浄化槽であれば良いものである。尚、ここでは、前記
沈殿分離槽N1、嫌気濾床槽N2等、被処理水を嫌気的
に生物処理する水処理槽を嫌気処理槽と総称するものと
する。また、前記嫌気処理槽と、前記膜分離槽E2との
間で、前記嫌気処理槽からの被処理水を移流自在に構成
した、脱窒槽E1、好気濾床槽等を総称して中間処理槽
と呼ぶものとする。[Another embodiment] In the above embodiment, the septic tank is
From the inlet I side, the sedimentation separation tank N1, the anaerobic filter bed tank N2,
The denitrification tank E1 and the membrane separation tank E2 are provided, but the present invention is not limited to this. For example, an aerobic filter bed that grows aerobic bacteria that aerobically treats water to be treated, instead of the anaerobic filter bed tank N2. May be provided to form a septic tank by providing an aerobic filter bed tank, which is simply a septic tank provided with an anaerobic treatment tank and a membrane separation tank E2. Here, water treatment tanks for anaerobically biologically treating the water to be treated, such as the sedimentation separation tank N1 and the anaerobic filter bed tank N2, are collectively referred to as anaerobic treatment tanks. Further, between the anaerobic treatment tank and the membrane separation tank E2, the denitrification tank E1, an aerobic filter bed tank, and the like, which are configured such that the water to be treated from the anaerobic treatment tank can freely flow therethrough, are collectively referred to as intermediate treatment. It shall be called a tank.
【0024】また、前記落下口3や、前記堰4aを総称
して流量設定部と呼び、しぼり弁等の流量制御手段を設
けて流量設定部を形成してあってもよい。Further, the fall port 3 and the weir 4a may be collectively called a flow rate setting section, and the flow rate setting section may be formed by providing flow rate control means such as a throttle valve.
【0025】また、先の実施例においては、膜分離装置
Mの一例として平膜を並設して構成したものを示した
が、これに限らず、中空糸膜等を用いたものでもよく、
これらを総称して膜分離装置と呼ぶものである。Further, in the above-described embodiment, an example in which flat membranes are arranged side by side is shown as an example of the membrane separation apparatus M. However, the present invention is not limited to this, and an apparatus using a hollow fiber membrane or the like may be used.
These are collectively called a membrane separation device.
【0026】前記返送管2の構成は先の構成によらず、
図3に示すように、返送口101を膜分離槽E2底部に
設け、前記脱窒槽E1内に設けた縦管112を前記返送
口に連通接続するとともに、前記縦管112の上端部に
横管122を連設して返送管102を構成し、前記返送
管102の前記縦管112に孔部103を形成して、前
記返送口101から前記孔部103までの部分をもっ
て、前記膜分離槽E2の被処理水を、膜分離槽E2の被
処理水をオーバーフローで前記中間処理槽へ返送する第
一返送路131を形成し、前記返送口101から前記横
管122の先端部開口122bまでの部分をもって膜分
離槽E2の被処理水をオーバーフローで前記嫌気処理槽
へ返送する第二返送路132を形成して、主に膜分離槽
E2底部の沈殿汚泥を大量に含む被処理水を、前記中間
処理槽や、嫌気処理槽に返送する構成にしてあってもよ
い。尚、図3の構成においては、返送管102の内部流
路における縦管112と横管122の接合部104から
被処理水がオーバーフロー返送されているものとし、前
記縦管112と横管122の接合部104を前記孔部1
03よりもやや高位置に設定して流量設定部を構成して
いるものとする。The structure of the return pipe 2 does not depend on the above structure.
As shown in FIG. 3, a return port 101 is provided at the bottom of the membrane separation tank E2, a vertical pipe 112 provided in the denitrification tank E1 is connected to the return port, and a horizontal pipe is provided at the upper end of the vertical pipe 112. The return pipe 102 is formed by connecting the return pipe 122 to the vertical pipe 112 of the return pipe 102, and a hole 103 is formed in the vertical pipe 112. Forming a first return path 131 for returning the water to be treated in the membrane separation tank E2 to the intermediate treatment tank by overflow, and a portion from the return port 101 to the tip end opening 122b of the horizontal pipe 122. A second return path 132 for returning the water to be treated in the membrane separation tank E2 to the anaerobic treatment tank by overflowing is formed, and the water to be treated mainly containing a large amount of settled sludge at the bottom of the membrane separation tank E2 is converted to the intermediate water. Treatment tank and anaerobic treatment It may be each other in the configuration to be returned to. In the configuration of FIG. 3, it is assumed that the water to be treated is overflowing and returned from the joint 104 between the vertical pipe 112 and the horizontal pipe 122 in the internal flow path of the return pipe 102. The joint 104 is connected to the hole 1
It is assumed that the flow rate setting unit is configured to be set at a position slightly higher than 03.
【0027】また、前記被処理水返送口1、前記返送口
101等返送路を連通させる部分を返送部と総称する。Further, a portion that connects the return path such as the treated water return port 1 and the return port 101 is collectively referred to as a return section.
【0028】尚、特許請求の範囲の項に、図面との対照
を便利にするために符号を記すが、該記入により本発明
は添付図面の構成に限定されるものではない。In the claims, reference numerals are provided for convenience of comparison with the drawings, but the present invention is not limited to the configuration shown in the attached drawings.
【図1】浄化槽の縦断側面図FIG. 1 is a vertical side view of a septic tank.
【図2】浄化槽の返送管の断面図FIG. 2 is a sectional view of a return pipe of a septic tank.
【図3】別実施例における浄化槽の返送管の縦断側面図FIG. 3 is a longitudinal sectional side view of a return pipe of a septic tank according to another embodiment.
1 返送部 2 返送管 2a 一端 2b 他端 3 落下口 4a 堰 21 第一返送路 22 第二返送路 E1 中間処理槽 E2 膜分離槽 Ee 隔壁 M 膜分離装置 N1 嫌気処理槽 DESCRIPTION OF SYMBOLS 1 Return part 2 Return pipe 2a One end 2b Other end 3 Drop port 4a Weir 21 First return path 22 Second return path E1 Intermediate processing tank E2 Membrane separation tank Ee Partition wall M Membrane separation apparatus N1 Anaerobic processing tank
───────────────────────────────────────────────────── フロントページの続き (72)発明者 本田 和之 滋賀県甲賀郡甲西町高松2番地の1 株 式会社クボタ 滋賀工場内 (72)発明者 浜田 勝己 滋賀県甲賀郡甲西町高松2番地の1 株 式会社クボタ 滋賀工場内 (56)参考文献 特開 平4−354592(JP,A) 特開 平4−354589(JP,A) 特開 平7−290075(JP,A) 特開 平5−337481(JP,A) 実開 平4−99295(JP,U) (58)調査した分野(Int.Cl.7,DB名) C02F 3/00 ZAB C02F 1/44 ZAB C02F 3/12 ZAB C02F 3/28 ZAB ──────────────────────────────────────────────────続 き Continuing from the front page (72) Inventor Kazuyuki Honda 1 at 2, Takamatsu, Kosai-cho, Koga-gun, Koka-gun, Shiga Prefecture Inside the Kubota Shiga Plant (72) Katsumi Hamada 2, Takamatsu, Kosai-cho, Koga-gun, Shiga 1 Kubota Corporation Shiga Plant (56) References JP-A-4-354592 (JP, A) JP-A-4-354589 (JP, A) JP-A-7-290075 (JP, A) JP-A-5 −337481 (JP, A) Japanese Utility Model 4-99295 (JP, U) (58) Fields investigated (Int. Cl. 7 , DB name) C02F 3/00 ZAB C02F 1/44 ZAB C02F 3/12 ZAB C02F 3/28 ZAB
Claims (3)
(M)を内装してなる膜分離槽(E2)とを備え、前記
嫌気処理槽(N1)と、膜分離槽(E2)との間に、嫌
気処理槽を経た被処理水を受ける中間処理槽(E1)を
設けてある浄化槽であって、 前記膜分離槽(E2)に被処理水を移送する移送ポンプ
(A)を前記中間処理槽(E1)に設け、前記膜分離槽
(E2)の被処理水を、オーバーフローで前記中間処理
槽(E1)へ返送する第一返送路(21)、及び、前記
膜分離槽(E2)の被処理水を、オーバーフローで前記
嫌気処理槽(N1)へ返送する第二返送路(22)を設
け、前記第一返送路(21)を介して前記中間処理槽
(E1)へ返送される被処理水が設定量を超過したとき
に、その設定量を超過する被処理水を前記第二返送路
(22)を介して前記嫌気処理槽(N1)へ返送するた
めの流量設定部を設けた浄化槽。An anaerobic treatment tank (N1) and a membrane separation tank (E2) containing a membrane separation device (M) are provided. The anaerobic treatment tank (N1), the membrane separation tank (E2) A purification tank provided with an intermediate treatment tank (E1) for receiving the water to be treated that has passed through the anaerobic treatment tank, wherein the transfer pump (A) for transferring the treatment water to the membrane separation tank (E2) is A first return path (21) provided in the intermediate treatment tank (E1) for returning the water to be treated in the membrane separation tank (E2) to the intermediate treatment tank (E1) by overflow; and the membrane separation tank (E2). A) a return line (22) for returning the water to be treated to the anaerobic treatment tank (N1) by overflow, and returned to the intermediate treatment tank (E1) via the first return path (21). When the treated water exceeds the set amount, the treated water exceeding the set amount is returned to the second (22) septic tank provided with a flow rate setting portion for returning the anaerobic treatment tank to (N1) via the.
被処理水の返送部(1)を設け、前記返送部(1)と前
記嫌気処理槽とにわたって返送管(2)を架設し、その
返送管(2)の一端(2a)を前記返送部(1)に接続
して、前記返送管(2)における前記返送部(1)から
前記返送管(2)の他端(2b)までの部分に第二返送
路(22)を形成するとともに、前記返送管(2)の中
間部で前記中間処理槽上方に被処理水を落下させる落下
口(3)を形成して流量設定部を構成し、かつ、前記返
送管(2)における前記返送部(1)から前記落下口
(3)までの部分に第一返送路(21)を形成してある
請求項1に記載の浄化槽。2. A return section (1) for water to be treated is provided on a partition wall (Ee) of the membrane separation tank (E1), and a return pipe (2) is installed between the return section (1) and the anaerobic treatment tank. Then, one end (2a) of the return pipe (2) is connected to the return section (1), and the return section (1) in the return pipe (2) is connected to the other end (2b) of the return pipe (2). ), A second return path (22) is formed, and a drop port (3) for dropping the water to be treated is formed above the intermediate treatment tank at an intermediate portion of the return pipe (2) to set the flow rate. 2. The septic tank according to claim 1, wherein a first return path (21) is formed in a part of the return pipe (2) from the return section (1) to the drop port (3). .
流れる被処理水の最大流量を設定する堰(4a)を設け
た請求項2に記載の浄化槽。3. The septic tank according to claim 2, wherein the flow rate setting section is provided with a weir (4a) for setting a maximum flow rate of the water to be treated flowing in the first return path (21).
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP24613194A JP3106066B2 (en) | 1994-10-12 | 1994-10-12 | Septic tank |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP24613194A JP3106066B2 (en) | 1994-10-12 | 1994-10-12 | Septic tank |
Publications (2)
Publication Number | Publication Date |
---|---|
JPH08141585A JPH08141585A (en) | 1996-06-04 |
JP3106066B2 true JP3106066B2 (en) | 2000-11-06 |
Family
ID=17143946
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP24613194A Expired - Fee Related JP3106066B2 (en) | 1994-10-12 | 1994-10-12 | Septic tank |
Country Status (1)
Country | Link |
---|---|
JP (1) | JP3106066B2 (en) |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP0970922B1 (en) * | 1998-07-06 | 2007-09-05 | Kubota Corporation | Method for methane fermentation of organic waste |
JP4734160B2 (en) * | 2006-04-13 | 2011-07-27 | 株式会社Gsユアサ | Septic tank |
CN102603124B (en) * | 2012-03-31 | 2013-06-12 | 华南理工大学 | Two-phase two-period anaerobic organism reactor for processing wastewater |
CN103626291B (en) * | 2013-11-28 | 2015-09-09 | 常州大学 | Internal-circulation type membrane bioreactor |
-
1994
- 1994-10-12 JP JP24613194A patent/JP3106066B2/en not_active Expired - Fee Related
Also Published As
Publication number | Publication date |
---|---|
JPH08141585A (en) | 1996-06-04 |
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