JPS61146397A - Method and apparatus for treating night soil - Google Patents
Method and apparatus for treating night soilInfo
- Publication number
- JPS61146397A JPS61146397A JP59267725A JP26772584A JPS61146397A JP S61146397 A JPS61146397 A JP S61146397A JP 59267725 A JP59267725 A JP 59267725A JP 26772584 A JP26772584 A JP 26772584A JP S61146397 A JPS61146397 A JP S61146397A
- Authority
- JP
- Japan
- Prior art keywords
- activated sludge
- human waste
- liquid
- treated
- treatment tank
- 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
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
- Activated Sludge Processes (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、活性汚泥処理方法と限外濾過方法とを組み合
わせ念し尿処理方法及びその装置に関する。DETAILED DESCRIPTION OF THE INVENTION [Industrial Field of Application] The present invention relates to a human urine treatment method that combines an activated sludge treatment method and an ultrafiltration method, and an apparatus therefor.
有機性物質を多量に含むし尿処理において従来の活性汚
泥処理方法、例えば低希釈2段活性汚泥法として標準化
されている方法は第4図に示す次のようなものである@
処理すべきし尿を受は入れ、し渣を除去した後、貯留し
く受入貯留工程)、活性汚泥に対する負荷を調整あるい
は軽減するためにし尿(以下原液とする)を希釈しく希
釈調整工程)、希釈された原液を活性汚泥槽において活
性汚泥処理上
さWる(活性汚泥処理工程)。この場合処理工程は2段
階に亘っておシ、第1段階として第1攪拌及び第1曝気
工程、第2段階として第2攪拌及び第2曝気工程とを備
えている。また、第1曝気工程を経穴処理液は循環液と
して希釈調整工程に循環される。The conventional activated sludge treatment method for treating human waste containing a large amount of organic substances, such as the standard low dilution two-stage activated sludge method, is as shown in Figure 4. After removing the sludge, it is stored (receiving and storage process), the dilution adjustment process (dilution adjustment process) in which the human waste (hereinafter referred to as the undiluted solution) is diluted to adjust or reduce the load on activated sludge, and the diluted sludge is activated. Activated sludge treatment is carried out in the sludge tank (activated sludge treatment process). In this case, the treatment process includes two stages: the first stage includes a first stirring and first aeration process, and the second stage includes a second stirring and second aeration process. Moreover, the acupuncture point treatment liquid in the first aeration process is circulated as a circulating liquid to the dilution adjustment process.
次に活性汚泥処理工程からの処理液を沈殿分離すること
によって懸濁物を分離しく沈殿分離工程、この場合、沈
殿分離された汚泥の一部は返送汚泥として希釈調整工程
に返送される。また分離された汚泥の他部は余剰汚泥と
して、脱水後系外に排出されるとともに、分離液は希釈
調整工程に返送される)、更に沈殿分離処理水に凝集剤
を投入し、処理水中の微細粒子を凝集沈殿させ(凝集分
離工程、この場合、凝集分離された汚泥は、脱水後系外
に排出されるとともに分離液は希釈調整工程に返送され
る)0次に浮遊固形物を除去しく砂−過工程)、更に溶
解物質を活性炭によって除去しく活性炭吸着工程)、消
毒して(消毒工程)放流される。Next, the treated liquid from the activated sludge treatment step is subjected to sedimentation separation to separate suspended matter, and in this case, a part of the sedimented sludge is returned to the dilution adjustment step as return sludge. The other part of the separated sludge is discharged as surplus sludge to the outside of the system after dewatering, and the separated liquid is returned to the dilution adjustment process. Fine particles are coagulated and precipitated (coagulation separation process, in this case, the coagulated and separated sludge is discharged outside the system after dehydration, and the separated liquid is returned to the dilution adjustment process).Next, suspended solids are removed. (sand filtering process), then the dissolved substances are removed by activated carbon (activated carbon adsorption process), and disinfected (disinfection process) before being discharged.
上述したように従来のし尿処理方法においては、放流水
の水質規準を満足するために多くの工程を必要とし、且
つこれらの工程ごとの槽あるいは装置を必要としている
ために次のような欠点がある。As mentioned above, conventional human waste treatment methods require many steps in order to meet the water quality standards for effluent water, and require tanks or equipment for each of these steps, resulting in the following drawbacks: be.
工程数が多いために運転管理が複雑で1)手間がかかる
・
固液分離工程として沈殿分離工程、凝集分離工程及び砂
濾過工程を採用しているため、また他方で原液を10倍
程度に希釈して処理するため、処理装置(活性汚泥処理
槽及び沈殿槽等)が大型化する。従って比較的広い敷地
面積及び大きな建設費が要求されている。また、原液を
希釈する希釈水の量が多いためその入手の困難さととも
に、放流水量が多くなシ放流水中の規制成分濃度は規制
値を満足してもこの規制成分の放流絶対量が多い。更に
、活性汚泥処理液を沈殿槽を用いて固液分離する際に活
性汚泥がバルキングを生じ、運転上支障をきたすことが
ある。Due to the large number of processes, operation management is complicated and 1) time-consuming. As the solid-liquid separation process uses precipitation separation process, coagulation separation process, and sand filtration process, on the other hand, the stock solution must be diluted about 10 times. Therefore, the processing equipment (activated sludge treatment tank, settling tank, etc.) becomes larger. Therefore, a relatively large site area and large construction costs are required. Furthermore, since the amount of dilution water used to dilute the stock solution is large, it is difficult to obtain it, and even if the concentration of the regulated component in the effluent water is large, even if the concentration of the regulated component satisfies the regulated value, the absolute amount of the regulated component released is large. Furthermore, when the activated sludge treatment liquid is subjected to solid-liquid separation using a settling tank, bulking may occur in the activated sludge, which may cause operational problems.
本発明は上述した事情に鑑みなされたもので、工程数が
少なく、所要敷地面積が小さく、原液を希釈する必要が
なく、小型で安価であ夛、しかも放流水中の規制成分の
濃度及び絶対量が少なく、バルキングによって運転に支
障をきたすことのないし尿処理方法及びその装置を提供
するものである。以下に、一実施例に基づき、第1図〜
第3図を参照して本発明の構成及び作用を説明する。The present invention has been made in view of the above-mentioned circumstances, and has a small number of steps, a small site area, no need to dilute the stock solution, is small and inexpensive, and is capable of controlling the concentration and absolute amount of regulated components in effluent water. The object of the present invention is to provide a method and apparatus for treating human waste that has a small amount of waste and does not interfere with operation due to bulking. Below, based on one example, FIGS.
The structure and operation of the present invention will be explained with reference to FIG.
本発明によるし尿処理方法は、複数の室より構成される
前段の活性汚泥処理槽の各室で、供給されたし尿を順次
活性汚泥処理させる前系列処理工程と、前記前段の活性
汚泥処理槽内の処理液を循環させる循環工程と、前記前
段の活性汚泥処理槽に処理すべきし尿を供給する供給工
程と、複数の室よ)構成される後段の活性汚泥処理槽の
各室で前記前段の活性汚泥処理槽からの処理液を順次活
性汚泥処理させる後系列処理工程と、前記後段の活性汚
泥処理槽からの処理液を限外濾過膜を有する限外−過装
置によって濾過し、P液と濃縮液とに分離し、濃縮液は
、その一部を前記前段及び後段の活性汚泥処理槽に返送
し、濃縮液の他部を余剰汚泥として回収し、F液はその
一部を前記後段の活性汚泥処理槽に返送し、F液の他部
を放流水として放流する限外−過工程とを備えている。The human waste treatment method according to the present invention includes a pre-sequence treatment step in which the supplied human waste is sequentially treated with activated sludge in each chamber of a pre-stage activated sludge treatment tank that is composed of a plurality of chambers, and a a circulation step for circulating the treated liquid, a supply step for supplying the human waste to be treated to the activated sludge treatment tank in the earlier stage, and a supply step for supplying human waste to be treated to the activated sludge treatment tank in the earlier stage; A post-sequence treatment step in which the treated liquid from the activated sludge treatment tank is sequentially treated with activated sludge, and the treated liquid from the latter stage activated sludge treatment tank is filtered by an ultra-filtration device having an ultrafiltration membrane, and P liquid and A part of the concentrated liquid is returned to the activated sludge treatment tanks in the earlier and later stages, the other part of the concentrated liquid is recovered as surplus sludge, and a part of the F liquid is returned to the activated sludge treatment tanks in the latter stage. It is equipped with an ultrafiltration process in which the F liquid is returned to the activated sludge treatment tank and the other part of the F liquid is discharged as effluent water.
本発明によるし尿処理装置は、複数の室より構成され、
し尿を順次各室で活性汚泥処理させる前段の活性汚泥処
理槽と、前記前段の活性汚泥処理槽内の処理液を循環さ
せる循環手段と、前記前段の活性汚泥処理槽にし尿を供
給する供給手段と、複数の室より構成され、前記前段の
活性汚泥処理槽からの処理液を各室で順次活性汚泥処理
させる後段の活性汚泥処理槽と、前記後段の活性汚泥処
理槽からの処理液を限外濾過膜によって濾過し、F液と
濃縮液とに分離し、濃縮液はその一部を前記前段及び後
段の活性汚泥処理槽に返送し、濃縮液の他部は余剰汚泥
として回収し、原液はその一部を前記後段処理槽に返送
し、F液の他部を放流水として放流する限外濾過装置と
を備えている。The human waste processing device according to the present invention is composed of a plurality of chambers,
A first activated sludge treatment tank for treating human waste with activated sludge in each chamber sequentially, a circulation means for circulating a treatment liquid in the first stage activated sludge treatment tank, and a supply means for supplying night soil to the first stage activated sludge treatment tank. and a downstream activated sludge treatment tank, which is composed of a plurality of chambers, in which the treated liquid from the preceding activated sludge treatment tank is sequentially treated with activated sludge in each chamber, and a downstream activated sludge treatment tank that restricts the treated liquid from the downstream activated sludge treatment tank. It is filtered through an outer filtration membrane and separated into liquid F and concentrated liquid. Part of the concentrated liquid is returned to the activated sludge treatment tanks in the previous and subsequent stages, and the other part of the concentrated liquid is recovered as surplus sludge and used as the undiluted solution. is equipped with an ultrafiltration device that returns a part of the F liquid to the latter treatment tank and discharges the other part as discharge water.
まず、第1図で、バキユーム車等によっテ収集きれたし
尿(以下原液とする)は受入槽4に受は入れられ、受入
槽4で原液に含まれている比較的大きな砂、石等が沈降
によって除去される。受入槽4はスクリーン10及び微
細目スクリーン12を介して貯留槽8に接続されている
。First, in Fig. 1, the human waste (hereinafter referred to as the undiluted solution) that has been completely collected by a vacuum vehicle, etc. is received in the receiving tank 4, and the relatively large sand, stones, etc. contained in the undiluted solution are received in the receiving tank 4. is removed by sedimentation. The receiving tank 4 is connected to the storage tank 8 via a screen 10 and a fine screen 12.
微細目スクリーン12には目開き0.2■のスクリーン
が用いられ、スクリーン10及び微細目スクリーン12
を通過することによって、原液中の比較的微細な固形物
が除去される。各スクリーンを通過した原液は貯留槽8
に貯留される。The fine mesh screen 12 uses a screen with a mesh opening of 0.2■, and the screen 10 and the fine mesh screen 12
By passing through the liquid, relatively fine solids in the stock solution are removed. The stock solution that has passed through each screen is stored in a storage tank 8.
is stored in
貯留槽8において原液の濃度の均一化が図られる。In the storage tank 8, the concentration of the stock solution is made uniform.
原液を前段処理槽18に供給するに先だち活性汚泥への
負荷の軽減と限外濾過膜の保護をはかるために原液中の
不溶性固形物(し渣)を除去することが好ましい。この
場合、スクリーンに原液を通過させてし渣を除去するが
、目開きの大きなスクリーンと目開きの小さなスクリー
ンとを組み合わせて用いることが好ましい。目開きの小
さなスクリーンは比較的微細な固形物量ソ除去するため
に目開き0.1m乃至0.5mの微細目スクリーンを用
いることが好ましい。Prior to supplying the stock solution to the pretreatment tank 18, it is preferable to remove insoluble solids (sludge) from the stock solution in order to reduce the load on the activated sludge and protect the ultrafiltration membrane. In this case, the undiluted solution is passed through a screen to remove the residue, and it is preferable to use a combination of a screen with large openings and a screen with small openings. It is preferable to use a screen with a small opening of 0.1 m to 0.5 m in order to remove a relatively fine amount of solid matter.
し尿の対象としては例えば、汲み取シし尿(BOD 1
3,500ダ/)程度)、し尿浄化槽汚泥(BOD 7
,000■/!程度)、し尿消化槽脱離液(BOD 2
,400■/l程度)等が挙げられる。Examples of human waste include collected human waste (BOD 1
3,500 da/)), human waste septic tank sludge (BOD 7)
,000■/! degree), human waste digester desorbed fluid (BOD 2
, 400 ■/l), etc.
ま(実質的に希釈されることなく)、ポンプ14によっ
て活性汚泥処理槽16に30017日(Q)で送られる
。(without being substantially diluted) is sent to the activated sludge treatment tank 16 by the pump 14 at 30,017 days (Q).
活性汚泥処理槽16は、7つの室(16)、。The activated sludge treatment tank 16 has seven chambers (16).
16B、16C,16D、16E、16F。16B, 16C, 16D, 16E, 16F.
16G)に区画されている。16G).
との処理槽16は、原液が流入される第1室16kから
第4室16Dまでの前段処理槽18と、第5室16Eか
ら処理液を流出する第7室16G−4での後段処理槽2
0とに区分されている。The processing tanks 16 include a pre-processing tank 18 from the first chamber 16k to the fourth chamber 16D into which the stock solution flows, and a post-processing tank 18 in the seventh chamber 16G-4 from which the processing liquid flows out from the fifth chamber 16E. 2
It is divided into 0 and 0.
各室は底部から上方に向けて延出する仕切シ壁によって
各室の処理液の液位が順次第1室16Aから第7室16
Gに沿って階段状に低くなるように区切られている。従
って第1室16kから第7室16Gへ処理液がオーバー
フローによって順次移動する。前段処理槽18は、複数
の室に区画されていれば、例えば3つ4つ等いくつの室
に区画されていても良い。Each chamber is divided by a partition wall extending upward from the bottom so that the liquid level of the processing liquid in each chamber is adjusted sequentially from chamber 1 16A to chamber 7 16.
It is divided into lower sections along the G line in a step-like manner. Therefore, the processing liquid sequentially moves from the first chamber 16k to the seventh chamber 16G due to overflow. The pre-processing tank 18 may be divided into any number of chambers, such as three or four, as long as it is divided into a plurality of chambers.
変形例として第2図に示すように、処理槽16は槽16
内の底部を基端としてここから上方に向けて延出する第
1の仕切シ壁17Aと、槽16内の天井部を基端として
ここから下方に向けて延出する第2の仕切シ壁17Bと
が交互に設けられていて、空気を第1室16A、第3室
16Cおよび第5室16Hに供給することによって好気
性に設定された第1室16kから嫌気性に設定された第
2室16Bへ処理液をオーバーフローによって移動させ
ると共に嫌気性に設定された第2室16Bおよび第4室
16Dから好気性に設定された第3室16Cおよび第5
室16Eへ処理液を底部を流れて移動させても良い。As a modified example, as shown in FIG.
A first partition wall 17A extends upward from the bottom of the tank 16 as a base end, and a second partition wall 17A extends downward from here with the ceiling of the tank 16 as a base end. 17B are provided alternately, and by supplying air to the first chamber 16A, the third chamber 16C, and the fifth chamber 16H, the first chamber 16k is set to be aerobic, and the second chamber 16k is set to be anaerobic. The processing liquid is moved by overflow to the chamber 16B, and from the second chamber 16B and the fourth chamber 16D, which are set to be anaerobic, to the third chamber 16C and the fifth chamber, which are set to be aerobic.
The processing liquid may be moved to the chamber 16E by flowing through the bottom.
また処理槽16には、第3図に示すように消泡スプレー
43が設けられていても良い。即ち、活性汚泥処理槽は
、高負荷処理の為、各室内で発泡することがらシ、泡が
溢流して隣室以降の室へ短絡し、処理効率が低下するこ
とがあるので泡の発生を防止するためである。この場合
、更に、各室の仕切シ板46の溢流部付近に邪魔板48
を設け、邪魔板と邪魔板との間に消泡スプレー43が併
設されていてもよい。この構成によって隣室への泡の流
入が防止される。Further, the processing tank 16 may be provided with a defoaming spray 43 as shown in FIG. In other words, since the activated sludge treatment tank performs high-load processing, foaming may occur in each chamber, and bubbles may overflow and short-circuit to subsequent rooms, reducing treatment efficiency, so prevent foaming from occurring. This is to do so. In this case, a baffle plate 48 is also provided near the overflow part of the partition plate 46 of each room.
may be provided, and a defoaming spray 43 may be provided between the baffle plates. This configuration prevents bubbles from flowing into adjacent rooms.
第1図に戻って前段処理槽18において、第1室16に
と第4室16Dとは、循環パイプ24によって接続され
ている。循環パイプ24には、第4室16D内の処理液
の一部を第1室16人へ循環するための循環ポンプ22
が介在されている。一方、貯留槽8は循環ポンプ22の
吸込み側で循環パイf24に接続されている。Returning to FIG. 1, in the pre-treatment tank 18, the first chamber 16 and the fourth chamber 16D are connected by a circulation pipe 24. The circulation pipe 24 includes a circulation pump 22 for circulating a part of the processing liquid in the fourth chamber 16D to the 16 people in the first chamber.
is mediated. On the other hand, the storage tank 8 is connected to the circulation pipe f24 on the suction side of the circulation pump 22.
従って貯留槽8からの原液は循環されている処理液に混
合されながら活性汚泥処理槽16に流量Qで送入される
。Therefore, the raw solution from the storage tank 8 is sent to the activated sludge treatment tank 16 at a flow rate Q while being mixed with the circulating treatment liquid.
第1室16Aにおいて循環ノぐイブ24の先端には、原
液と循環液の混合液を送入する際に空気を導入するため
の曝気インジェクター(商品名:三井−バイニルインジ
ェクタ一式散気装置)26が設けられている。また、こ
の循環ポンプ22によって最大120Qの処理液が循環
されている。本実施例では約40Qで循環されている。At the tip of the circulation nozzle 24 in the first chamber 16A, there is an aeration injector (product name: Mitsui Vinyl Injector Complete Aeration Device) for introducing air when feeding the mixture of stock solution and circulating fluid. 26 are provided. Furthermore, the circulation pump 22 circulates a maximum of 120Q of processing liquid. In this embodiment, the cycle is approximately 40Q.
活性汚泥槽16に送入された原液は循環液とともに第1
室16kから順次オーバーフローしながら各室を通過し
、第7室に達する。第2室16B、第3室16C1第4
室16D1第6室16F及び第7室16Gには夫々空気
を供給するために通常用いられている曝気装置30,3
1゜32.36.38が設置されている。これらの曝気
装置には供給する空気量を独立して調節するための調節
器(図示されず)が設けられている。第1室16A及び
第5室16Eが嫌気性雰囲気に保持され、第2、第3、
第4、第6、そして第7室16B、16C,16D、1
6F。The raw solution sent to the activated sludge tank 16 is sent to the first tank together with the circulating fluid.
Starting from the chamber 16k, the water passes through each chamber while overflowing and reaches the seventh chamber. 2nd chamber 16B, 3rd chamber 16C1 4th
The chamber 16D1, the sixth chamber 16F, and the seventh chamber 16G are equipped with aeration devices 30, 3, which are normally used for supplying air, respectively.
1°32.36.38 is installed. These aeration devices are equipped with regulators (not shown) for independently regulating the amount of air supplied. The first chamber 16A and the fifth chamber 16E are maintained in an anaerobic atmosphere, and the second, third,
4th, 6th, and 7th chambers 16B, 16C, 16D, 1
6F.
および16Gは好気性雰囲気に保持されている。and 16G are maintained in an aerobic atmosphere.
原液が前段処理槽に供給される際には、前段処理槽内で
循環されている処理液(循環液)に原液を混合すること
が好ましい。When the stock solution is supplied to the pre-processing tank, it is preferable to mix the stock solution with the processing liquid (circulating liquid) that is being circulated within the pre-processing tank.
処理液が循環しているラインには、処理液が流れる方向
の先端に曝気インジェクターが設けられているので、こ
の場合処理液に空気が導入る。Since an aeration injector is provided at the tip of the line in which the processing liquid is circulated in the direction in which the processing liquid flows, air is introduced into the processing liquid in this case.
各室には、夫々空気の供給量が調節可能な曝気装置が配
設され、各室に供給する空気量を任意に調節することに
よって各室の雰囲気を相対的に好気性または嫌気性に任
意に独立して設定可能である。この場合、例えば各室の
雰囲気を好気性と嫌気性とに交互に設定することもでき
る。Each room is equipped with an aeration device that can adjust the amount of air supplied to each room, and by arbitrarily adjusting the amount of air supplied to each room, the atmosphere in each room can be made relatively aerobic or anaerobic. can be set independently. In this case, for example, the atmosphere in each room can be set alternately to aerobic and anaerobic.
原液を前段処理槽に供給する際には、原液は希釈する必
要がない。There is no need to dilute the stock solution when supplying it to the pre-treatment tank.
供給工程において原液は、前段処理槽に供給される際、
1つの室に供給されることに限らない。例えば第2図の
ように室が3つ以上に区画されている場合、第1及び第
3の室に同時に供給しても良い。後段処理槽20の各室
は、前段処理槽と同様に、複数であればいくつの室に区
画されていても良く相対的に好気性または嫌気性の雰囲
気に任意に独立して設定可能であることが好ましい。し
かも、本実施例の如く後段処理槽内の処理液を限外濾過
装置へ供給゛するための最後の室及び最後から2番目の
室は好気性に設定されることが好ましい。との場合、粘
着性を有する嫌気性菌が、限外濾過膜の直前で増殖され
ないから、限外濾過膜にこれらの菌が付着することによ
って生じる濾過性能の低下を防止し、膜の洗滌回数を減
することができる。処理槽16において前段槽18及び
後段槽20には、嫌気性室と好気性室とが設定され、こ
れら嫌気性雰囲気および好気性雰囲気の組み合せによっ
て効果的にし尿が活性汚泥処理される。In the supply process, when the stock solution is supplied to the pre-treatment tank,
It is not limited to being supplied to one chamber. For example, when the chamber is divided into three or more as shown in FIG. 2, the first and third chambers may be supplied at the same time. Each chamber of the post-processing tank 20, like the pre-processing tank, may be divided into any number of chambers as long as it is plural, and can be independently set to a relatively aerobic or anaerobic atmosphere. It is preferable. Furthermore, as in this embodiment, it is preferable that the last chamber and the second to last chamber for supplying the treated liquid in the subsequent treatment tank to the ultrafiltration device are set to be aerobic. In this case, sticky anaerobic bacteria are not grown immediately before the ultrafiltration membrane, which prevents a decrease in filtration performance caused by the adhesion of these bacteria to the ultrafiltration membrane, and reduces the number of times the membrane is washed. can be reduced. In the treatment tank 16, an anaerobic chamber and an aerobic chamber are set in the first stage tank 18 and the second stage tank 20, and the combination of these anaerobic atmospheres and aerobic atmospheres effectively processes human waste into activated sludge.
第7室はパイプ39及び循環ポンプ40を介して限外濾
過装置42に接続されている。限外濾過装置42には、
ポリアクリロニトリル製分画分子量15,000乃至2
0,000の限外濾過膜、。−’Alf −5y社製ア
イ1,7■2,8ゎヨうわている。処理液は限外濾過膜
に対してクロスフロ一方式で流されp液と濃縮液とに分
離される。The seventh chamber is connected to an ultrafiltration device 42 via a pipe 39 and a circulation pump 40. The ultrafiltration device 42 includes:
Polyacrylonitrile molecular weight cutoff 15,000 to 2
0,000 ultrafiltration membrane,. -'Alf -5y Eye 1, 7, 2, 8 is waving. The treated liquid is passed through the ultrafiltration membrane in a cross-flow manner and separated into a p liquid and a concentrated liquid.
限外濾過膜によシ限外濾過装置42は汚液パイプ43を
介して活性炭層44に接続されている。An ultrafiltration device 42 using an ultrafiltration membrane is connected to an activated carbon layer 44 via a dirty liquid pipe 43.
汚液パイプからはF液の一部を第7室に戻すためのF液
返送・ぐイブ45が分枝されている。更に、限外濾過装
置42からはその濃縮液を前段槽16の第4室16D及
び後段槽18の第7室16Gに返送するための返送ノ々
イブ46が配設されている。返送ノソイf46からは濃
縮液の残部を余剰汚泥として系外に排出するための余剰
汚泥i4イデ48が分枝されている。上記汚液の一部(
Q)は活性炭層44を通過させることによってP液中の
溶解物質を除去した後、放流水として放流され、F液の
他部(約0.2Q)はバイア’45を介して第7室16
Gに戻される。An F liquid return pipe 45 for returning part of the F liquid to the seventh chamber is branched from the dirty liquid pipe. Furthermore, a return nozzle 46 is provided for returning the concentrated liquid from the ultrafiltration device 42 to the fourth chamber 16D of the first stage tank 16 and the seventh chamber 16G of the second stage tank 18. An excess sludge i4 ide 48 is branched from the return flow f46 to discharge the remainder of the concentrated liquid as excess sludge to the outside of the system. Part of the above sewage (
After Q) passes through the activated carbon layer 44 to remove dissolved substances in the P liquid, it is discharged as effluent water, and the other part (approximately 0.2Q) of the F liquid passes through the via '45 to the seventh chamber 16.
Returned to G.
一方濃縮液は前段槽18の第4室16D及び後段槽20
の第7室16Gに各々流量的10Q及び約60Qで返送
される。On the other hand, the concentrated liquid is stored in the fourth chamber 16D of the front stage tank 18 and the rear stage tank 20.
are returned to the seventh chamber 16G at a flow rate of about 10Q and about 60Q, respectively.
限外濾過膜は、分画分子量1,000乃至300万の範
囲のものが用いられる。The ultrafiltration membrane used has a molecular weight cut-off of 1,000 to 3,000,000.
限外濾過膜からのF液は、そのまま処理水として放流さ
れるが、汚液中の溶解物質を除去す限外濾過装置からの
濃縮液の一部は、活性汚泥濃度を制御し、且つ汚泥の活
性化を図るとともに難分解性物質を繰返し分解させるた
めに前段及び後段槽に通常20Q乃至120Qの範囲は
余剰汚泥として系外に取シ出される。後段処理槽(第7
室)の処理液を限外濾過装置42に供給し、ここで処理
液は濃縮液として高度に濃縮され、<シ返し前段及び後
段処理槽に返送されるので処理液中の難分解性有機物質
も活性汚泥によって繰シ返しあるいは長時間に亘って分
解される。The F solution from the ultrafiltration membrane is discharged as treated water as it is, but a part of the concentrate from the ultrafiltration device that removes dissolved substances in the sewage is used to control the activated sludge concentration and to In order to activate the sludge and repeatedly decompose the recalcitrant substances, sludge in the range of 20Q to 120Q is usually taken out of the system as surplus sludge in the front and rear tanks. Post-processing tank (7th
The treated liquid in the chamber) is supplied to the ultrafiltration device 42, where the treated liquid is highly concentrated as a concentrated liquid, and is returned to the pre- and post-processing tanks, so that hardly decomposable organic substances in the treated liquid are removed. It is also decomposed repeatedly or over a long period of time by activated sludge.
活性汚泥濃度を容易に高めることができなかったが、本
発明によれば沈殿槽を用いていないから活性汚泥濃度(
;jigs )を容易IC遍のることができ、高負荷高
濃度運転が可能である。例えば従来の活性汚泥濃度(M
L、8g >は4,000乃至8.000 my/lで
あったが、本発明では6,000乃至25.00011
19/lに設定さπ鷲。本実施例では12.000〜1
3,000〜ηに設定した。The activated sludge concentration could not be easily increased, but according to the present invention, since no settling tank is used, the activated sludge concentration (
;jigs) can be easily transferred to the IC, and high-load, high-concentration operation is possible. For example, the conventional activated sludge concentration (M
L, 8g > was 4,000 to 8.000 my/l, but in the present invention it was 6,000 to 25.00011
π Eagle set to 19/l. In this example, 12.000 to 1
It was set to 3,000 to η.
本発明は上述した範囲に限定されるととなく本発明の趣
旨を逸脱しない範囲で種々変形可能である。The present invention is not limited to the above-mentioned scope, but can be modified in various ways without departing from the spirit of the present invention.
この実施例によるし尿処理の結果を第1表を参照して説
明する。The results of human waste treatment according to this example will be explained with reference to Table 1.
第1図に示す貯留槽8において濃度を略均−に調整(希
釈されない)された原液、限外濾過膜を通過し九汚液及
び活性炭層44を通過した放流水を採取し夫々の水質、
即ち、BOD (生物化学的酸素要求量)、SS(浮遊
固形物)、C0D(化学的酸素要求量)、、T−N(総
窒素量)、大腸菌群数、そして色度を測定した。それら
の測定結果を第1表に示す。In the storage tank 8 shown in FIG. 1, the undiluted solution whose concentration has been adjusted to a substantially uniform level (not diluted), the sewage that has passed through the ultrafiltration membrane, and the discharged water that has passed through the activated carbon layer 44 are collected, and the quality of each water,
That is, BOD (biochemical oxygen demand), SS (suspended solids), C0D (chemical oxygen demand), TN (total nitrogen), coliform bacteria count, and chromaticity were measured. The measurement results are shown in Table 1.
第1表から明らかなように、本実施例では、従来の値を
下まわる良好な水質の放流水を得た。As is clear from Table 1, in this example, effluent water of good quality, which was lower than the conventional value, was obtained.
特に注目すべきことは、従来の方法では活性汚泥槽への
供給量及び放流量ダは共にIOQであるが、本実施例で
は原液を希釈していないため供給量及び放流量は共にQ
でありて、従来の約1710である。従って規制成分の
放流絶対量も従来の約1710である。尚、第1表に示
すBOD等の絶対量はQ=300J/日に対する値であ
る。What is particularly noteworthy is that in the conventional method, the supply amount and discharge amount to the activated sludge tank are both IOQ, but in this example, since the stock solution is not diluted, both the supply amount and the discharge amount are Q.
This is about 1710 compared to the conventional one. Therefore, the absolute discharge amount of the regulated component is also about 1710, which is the conventional value. Incidentally, the absolute amounts of BOD etc. shown in Table 1 are values for Q=300J/day.
少なく、運転が容易でsb大きな敷地面積が不要でsb
小型の装置で安価にし尿を処理することができる。Small size, easy to operate sb No need for large site area sb
Human waste can be processed at low cost with a small device.
即ち、原液を希釈する必要がないため(系外から希釈水
を導入する必要がないため)処理量及び放流量は、共に
Q(原液供給量に同じ)で従来の方法の約1710でア
シ、従って、放流水中の規制成分の濃度が従来方法と同
等としても放流水中の規制成分の絶対量も約1/10に
減少すると共に活性汚泥処理槽、ポンプ、配管等の装置
の各部を小屋にすることができる。In other words, since there is no need to dilute the stock solution (there is no need to introduce dilution water from outside the system), both the processing amount and the discharge amount are Q (same as the stock solution supply amount), which is about 1710 liters compared to the conventional method. Therefore, even if the concentration of the regulated components in the effluent is the same as in the conventional method, the absolute amount of the regulated components in the effluent is reduced to about 1/10, and each part of the equipment, such as the activated sludge treatment tank, pump, and piping, is reduced to a shed. be able to.
限外p過膜を用いているから放流水は浮遊固形物(88
)、病原菌、溶解高分子有機物等をほとんど含まない良
好な水質とすることができる。Since an ultrap filter membrane is used, the effluent water contains suspended solids (88
), the water quality can be made to be of good quality, containing almost no pathogenic bacteria, dissolved polymeric organic matter, etc.
従って従来方法の沈殿槽、凝集沈殿槽、砂濾過槽、更に
これらに関連する工程が不要であるから、処理装置の建
設費、敷地面積は大巾に低減するとともに、運転管理も
容易になる。例えば、一般に従来方法では活性汚泥処理
槽乃至砂濾過槽までの合計の容積は原液量Qに対して3
0Q程度に設計されるが、本発明によれば約7Q程度、
即ち従来方法の約174の容積にすることができる。Therefore, since the settling tank, coagulation sedimentation tank, sand filtration tank, and related processes of the conventional method are not necessary, the construction cost and site area of the treatment equipment are greatly reduced, and operation management is also facilitated. For example, in general, in conventional methods, the total volume from the activated sludge treatment tank to the sand filtration tank is 3
Although it is designed to be about 0Q, according to the present invention, it is about 7Q,
That is, the volume can be reduced to about 174 compared to the conventional method.
装置のフローパターンを示し要因、第2図は処理槽の他
の例を示す概略断面図、第3図は更に他の変形例による
処理槽の概略断面図、そして第4図は従来のし尿処理方
法を説明するための工程図である。Fig. 2 is a schematic sectional view showing another example of the processing tank, Fig. 3 is a schematic sectional view of a processing tank according to another modification, and Fig. 4 is a conventional human waste treatment. It is a process chart for explaining a method.
3・・・供給手段、18・・・前段処理槽、20・・・
後段処理槽、42・・・限外濾過装置。3... Supply means, 18... Pre-treatment tank, 20...
Post-processing tank, 42...ultrafiltration device.
出願人代理人 弁理士 鈴 江 武 彦特許庁長官
宇 賀 道 部 殿
特願昭59−267725号
2、発明の名称
し尿処理方法及びその装置
3、補正をする者
事件との関係 特許出願人
5、自発補正
7、補正の内容
(1) 明細書中第24頁第6行目に「することがで
きる。」とめる後に下記文を加入する。Applicant's agent Patent attorney Takehiko Suzue, Commissioner of the Patent Office
Michibe Uga, Patent Application No. 59-267725 2, Title of the invention: Human waste disposal method and its device 3, Relationship with the case of the person making the amendment Patent applicant 5, Spontaneous amendment 7, Contents of the amendment (1) Description In the 6th line of page 24, add the following sentence after ending ``It is possible.''
記
「また、一般に吸着剤としての活性炭層では、液体中の
浮遊固形物(SS)、水溶性有機物(COD)、無機塩
または燐酸イオン等を吸着するが、この実施例では限外
濾過膜を通過したF液を活性炭層に供給しているから、
活性炭層の目詰りまたは吸着i能低下の原因となるよう
な浮遊固形物及び高分子有機物を限外p過膜によって予
め除去できる。従って、この実施例によれば活性炭層の
性能を保持しつつ効率よく目的物を除去できる。」
う``In addition, activated carbon layers as adsorbents generally adsorb suspended solids (SS), water-soluble organic substances (COD), inorganic salts, phosphate ions, etc. in liquids, but in this example, an ultrafiltration membrane was used. Since the passed F liquid is supplied to the activated carbon layer,
Suspended solids and polymeric organic substances that may cause clogging of the activated carbon layer or decrease in adsorption capacity can be removed in advance by the ultrapolar membrane. Therefore, according to this embodiment, the target material can be efficiently removed while maintaining the performance of the activated carbon layer. " cormorant
Claims (1)
室で、供給されたし尿を順次活性汚泥処理させる前系列
処理工程と、前記前段の活性汚泥処理槽内の処理液を循
環させる循環工程と、前記前段の活性汚泥処理槽に処理
すべきし尿を供給する供給工程と、複数の室より構成さ
れる後段の活性汚泥処理槽の各室で前記前段の活性汚泥
処理槽からの処理液を、順次活性汚泥処理させる後系列
処理工程と、前記後段の活性汚泥処理槽からの処理液を
限外ろ過膜を有する限外ろ過装置によってろ過し、ろ液
と濃縮液とに分離し、濃縮液は、その一部を前記前段及
び後段の活性汚泥処理槽に返送し、濃縮液の他部を余剰
汚泥として回収し、ろ液はその一部を前記後段の活性汚
泥処理槽に返送し、ろ液の他部を放流水として放流する
限外ろ過工程とを備えるし尿処理方法。 2、前記循環工程において、処理液はポンプによって循
環され、前記供給工程において処理すべきし尿はそのポ
ンプの吸い込み側に供給され、し尿が処理液と混合され
ながら前段の活性汚泥処理槽に供給されることを特徴と
する特許請求の範囲第1項に記載のし尿処理方法。 3、前記循環工程において処理液は曝気インジェクター
を介して前段の活性汚泥処理槽に戻され、その曝気イン
ジェクターによって空気と混合されることを特徴とする
特許請求の範囲第1項あるいは第2項のいずれか1項に
記載のし尿処理方法。 4、前記前段及び後段の活性汚泥処理槽の各室は曝気イ
ンジェクターあるいはディフィーザによって曝気量が調
節され、任意に且つ独立して好気性あるいは嫌気性雰囲
気に保持されることを特徴とする特許請求の範囲第1項
ないし第3項のいずれか1項に記載のし尿処理方法。 5、前記供給工程において処理すべきし尿は希釈されな
いことを特徴とする特許請求の範囲第1項ないし第4項
のいずれか1項に記載のし尿処理方法。 6、前記前段及び後段の活性汚泥処理槽において活性汚
泥の濃度は6,000mg/l乃至25,000mg/
lに設定されることを特徴とする特許請求の範囲第1項
ないし第5項に記載のし尿処理方法。 7、前記後系列処理工程において、後段の活性汚泥処理
槽の最後及び最後から2番目の室を好気性雰囲気に保持
することを特徴とする特許請求の範囲第4項記載のし尿
処理方法。 8、複数の室より構成され、し尿を順次各室で活性汚泥
処理させる前段の活性汚泥処理槽と、前記前段の活性汚
泥処理槽内の処理液を循環させる循環手段と、前記前段
の活性汚泥処理槽にし尿を供給する供給手段と、複数の
室より構成され、前記前段の活性汚泥処理槽からの処理
液を各室で順次活性汚泥処理させる後段の活性汚泥処理
槽と、前記後段の活性汚泥処理槽からの処理液を限外ろ
過膜によってろ過し、ろ液と濃縮液とに分離し、濃縮液
はその一部を前記前段及び後段の活性汚泥処理槽に返送
し、濃縮液の他部は余剰汚泥として回収し、ろ液はその
一部を前記後段処理槽に返送し、ろ液の他部を放流水と
して放流する限外ろ過装置とを備えるし尿処理装置。 9、前記循環手段は処理液を循環させるためのポンプを
備え、前記供給手段は処理すべきし尿をそのポンプの吸
い入み側に供給する導管を備え、処理すべきし尿が処理
液と混合されながら前段の活性汚泥処理槽に供給される
ことを特徴とする特許請求の範囲第8項に記載のし尿処
理装置。 10、前記循環手段は、処理液を循環させるためのライ
ンを備え、その処理液が流れる方向のラインの先端には
曝気インジェクターが設けられ、処理液が前段の処理槽
に戻される際に曝気インジェクターによって空気と混合
されることを特徴とする特許請求の範囲第8項あるいは
第9項のいずれか1項に記載のし尿処理装置。 11、前記前段及び後段の活性汚泥処理槽の各室には、
曝気量を調節できる曝気インジェクターあるいはディフ
ューザーが設けられ、各室が任意に且つ独立して好気性
あるいは嫌気性雰囲気に保持されることを特徴とする特
許請求の範囲第8項ないし第10項のいずれか1項に記
載のし尿処理装置。 12、前記供給手段において処理すべきし尿は希釈され
ないことを特徴とする特許請求の範囲第8項ないし第1
1項のいずれか1項に記載のし尿処理装置。 13、前記前段及び後段の各室の活性汚泥濃度は、6,
000mg/l乃至25,000mg/lであることを
特徴とする特許請求の範囲第8項ないし第12項のいず
れか1項に記載のし尿処理装置。 14、前記後段の活性汚泥処理槽は、最後及び最後から
2番目の室を好気性雰囲気に保持してあることを特徴と
する特許請求の範囲第11項記載のし尿処理装置。[Scope of Claims] 1. A pre-sequence treatment step in which the supplied human waste is sequentially treated with activated sludge in each chamber of the pre-stage activated sludge treatment tank which is composed of a plurality of chambers, and a circulation step for circulating the treated solution, a supply step for supplying human waste to be treated to the activated sludge treatment tank in the previous stage, and a step in which the activated sludge treatment tank in the former stage is circulated in each chamber of the activated sludge treatment tank in the latter stage, which is composed of a plurality of chambers. A post-sequence treatment step in which the treated liquid from the sludge treatment tank is sequentially treated with activated sludge, and the treated liquid from the latter activated sludge treatment tank is filtered by an ultrafiltration device having an ultrafiltration membrane, and the filtrate and concentration are concentrated. Part of the concentrated liquid is returned to the activated sludge treatment tanks in the earlier and later stages, the other part of the concentrated liquid is recovered as surplus sludge, and part of the filtrate is returned to the activated sludge treatment tanks in the latter stage. A method for treating human waste comprising an ultrafiltration step of returning the filtrate to a sludge treatment tank and discharging the other part of the filtrate as effluent water. 2. In the circulation step, the treatment liquid is circulated by a pump, and in the supply step, the human waste to be treated is supplied to the suction side of the pump, and the human waste is mixed with the treatment liquid and supplied to the preceding activated sludge treatment tank. A human waste disposal method according to claim 1, characterized in that: 3. In the circulation step, the treatment liquid is returned to the activated sludge treatment tank at the previous stage via an aeration injector, and is mixed with air by the aeration injector. The human waste disposal method according to any one of the items. 4. The aeration amount of each chamber of the first and second activated sludge treatment tanks is adjusted by an aeration injector or a diffuser, and the chambers are arbitrarily and independently maintained in an aerobic or anaerobic atmosphere. The method for treating human waste according to any one of Items 1 to 3. 5. The human waste treatment method according to any one of claims 1 to 4, wherein the human waste to be treated is not diluted in the supply step. 6. The concentration of activated sludge in the first stage and second stage activated sludge treatment tanks is 6,000 mg/l to 25,000 mg/l.
6. The human waste processing method according to claim 1, wherein the human waste treatment method is set to l. 7. The human waste treatment method according to claim 4, wherein in the post-sequence treatment step, the last and penultimate chambers of the downstream activated sludge treatment tank are maintained in an aerobic atmosphere. 8. A pre-stage activated sludge treatment tank composed of a plurality of chambers, in which human waste is sequentially treated with activated sludge in each chamber, a circulation means for circulating the treatment liquid in the pre-stage activated sludge treatment tank, and the pre-stage activated sludge treatment tank. a supply means for supplying human waste to a treatment tank; a rear activated sludge treatment tank which is comprised of a plurality of chambers and sequentially processes the treated liquid from the earlier activated sludge treatment tank as activated sludge in each chamber; The treated liquid from the sludge treatment tank is filtered by an ultrafiltration membrane and separated into a filtrate and a concentrated liquid. A part of the concentrated liquid is returned to the activated sludge treatment tanks in the previous and subsequent stages, and other parts of the concentrated liquid are an ultrafiltration device for recovering part of the sludge as surplus sludge, returning a part of the filtrate to the latter treatment tank, and discharging the other part of the filtrate as effluent water. 9. The circulation means includes a pump for circulating the treatment liquid, and the supply means includes a conduit for supplying the human waste to be treated to the suction side of the pump, and the human waste to be treated is mixed with the treatment liquid. The human waste treatment apparatus according to claim 8, wherein the human waste is supplied to the activated sludge treatment tank in the preceding stage. 10. The circulation means includes a line for circulating the treatment liquid, and an aeration injector is provided at the tip of the line in the direction in which the treatment liquid flows, and when the treatment liquid is returned to the preceding treatment tank, the aeration injector is installed. The human waste treatment device according to any one of claims 8 and 9, characterized in that the human waste is mixed with air by. 11. In each chamber of the first stage and second stage activated sludge treatment tank,
Any one of claims 8 to 10, characterized in that an aeration injector or diffuser is provided that can adjust the amount of aeration, and each chamber is arbitrarily and independently maintained in an aerobic or anaerobic atmosphere. The human waste treatment device according to item 1. 12. Claims 8 to 1, characterized in that the human waste to be treated in the supply means is not diluted.
The human waste treatment device according to any one of Item 1. 13. The activated sludge concentration in each of the first and second chambers is 6.
13. The human waste treatment device according to any one of claims 8 to 12, characterized in that the amount of waste is 000 mg/l to 25,000 mg/l. 14. The human waste treatment apparatus according to claim 11, wherein the last and second to last chambers of the downstream activated sludge treatment tank are maintained in an aerobic atmosphere.
Priority Applications (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP59267725A JPH0630791B2 (en) | 1984-12-19 | 1984-12-19 | Human waste processing method and apparatus |
Applications Claiming Priority (1)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
JP59267725A JPH0630791B2 (en) | 1984-12-19 | 1984-12-19 | Human waste processing method and apparatus |
Related Child Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP61270377A Division JPS62117693A (en) | 1986-11-12 | 1986-11-12 | Decoloring method for night soil |
Publications (2)
Publication Number | Publication Date |
---|---|
JPS61146397A true JPS61146397A (en) | 1986-07-04 |
JPH0630791B2 JPH0630791B2 (en) | 1994-04-27 |
Family
ID=17448696
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
JP59267725A Expired - Lifetime JPH0630791B2 (en) | 1984-12-19 | 1984-12-19 | Human waste processing method and apparatus |
Country Status (1)
Country | Link |
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JP (1) | JPH0630791B2 (en) |
Cited By (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6328500A (en) * | 1986-07-21 | 1988-02-06 | Kurita Water Ind Ltd | Treatment device for night soil sanitary sewage |
JPH01168398A (en) * | 1987-12-24 | 1989-07-03 | Ebara Infilco Co Ltd | Waste water treatment at garbage incineration station |
JPH02135199A (en) * | 1988-11-14 | 1990-05-24 | Mitsui Eng & Shipbuild Co Ltd | Treatment of night soil |
JP2012192396A (en) * | 2010-07-21 | 2012-10-11 | Kurita Water Ind Ltd | Method and apparatus for biologically treating organic wastewater |
WO2013140925A1 (en) * | 2012-03-23 | 2013-09-26 | 水ing株式会社 | Treatment method and treatment device for oil-containing waste water |
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JPS4840971A (en) * | 1971-10-01 | 1973-06-15 | ||
JPS5198143A (en) * | 1975-02-26 | 1976-08-28 | ||
JPS5362360A (en) * | 1976-11-15 | 1978-06-03 | Osaka Gas Co Ltd | Method of treating active carbon for waste water |
JPS5496261A (en) * | 1978-01-13 | 1979-07-30 | Hitachi Chem Co Ltd | High-quality treatment of high-bod waste water |
JPS54102056A (en) * | 1978-01-27 | 1979-08-11 | Ebara Infilco Co Ltd | Process for high-speed treatment of waste water |
JPS5684697A (en) * | 1979-12-08 | 1981-07-10 | Ebara Infilco Co Ltd | Treatment of high concentration organic waste water |
JPS5799396A (en) * | 1980-12-08 | 1982-06-21 | Daido Steel Co Ltd | Treatment of waste water |
JPS5851988A (en) * | 1981-09-21 | 1983-03-26 | Nishihara Environ Sanit Res Corp | Slightly-diluting double-stage active sludge process |
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1984
- 1984-12-19 JP JP59267725A patent/JPH0630791B2/en not_active Expired - Lifetime
Patent Citations (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS4840971A (en) * | 1971-10-01 | 1973-06-15 | ||
JPS5198143A (en) * | 1975-02-26 | 1976-08-28 | ||
JPS5362360A (en) * | 1976-11-15 | 1978-06-03 | Osaka Gas Co Ltd | Method of treating active carbon for waste water |
JPS5496261A (en) * | 1978-01-13 | 1979-07-30 | Hitachi Chem Co Ltd | High-quality treatment of high-bod waste water |
JPS54102056A (en) * | 1978-01-27 | 1979-08-11 | Ebara Infilco Co Ltd | Process for high-speed treatment of waste water |
JPS5684697A (en) * | 1979-12-08 | 1981-07-10 | Ebara Infilco Co Ltd | Treatment of high concentration organic waste water |
JPS5799396A (en) * | 1980-12-08 | 1982-06-21 | Daido Steel Co Ltd | Treatment of waste water |
JPS5851988A (en) * | 1981-09-21 | 1983-03-26 | Nishihara Environ Sanit Res Corp | Slightly-diluting double-stage active sludge process |
Cited By (6)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS6328500A (en) * | 1986-07-21 | 1988-02-06 | Kurita Water Ind Ltd | Treatment device for night soil sanitary sewage |
JPH01168398A (en) * | 1987-12-24 | 1989-07-03 | Ebara Infilco Co Ltd | Waste water treatment at garbage incineration station |
JPH02135199A (en) * | 1988-11-14 | 1990-05-24 | Mitsui Eng & Shipbuild Co Ltd | Treatment of night soil |
JP2012192396A (en) * | 2010-07-21 | 2012-10-11 | Kurita Water Ind Ltd | Method and apparatus for biologically treating organic wastewater |
WO2013140925A1 (en) * | 2012-03-23 | 2013-09-26 | 水ing株式会社 | Treatment method and treatment device for oil-containing waste water |
JPWO2013140925A1 (en) * | 2012-03-23 | 2015-08-03 | 水ing株式会社 | Method and apparatus for treating wastewater containing oil |
Also Published As
Publication number | Publication date |
---|---|
JPH0630791B2 (en) | 1994-04-27 |
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