JP3136902B2 - Wastewater treatment method - Google Patents
Wastewater treatment methodInfo
- Publication number
- JP3136902B2 JP3136902B2 JP11577994A JP11577994A JP3136902B2 JP 3136902 B2 JP3136902 B2 JP 3136902B2 JP 11577994 A JP11577994 A JP 11577994A JP 11577994 A JP11577994 A JP 11577994A JP 3136902 B2 JP3136902 B2 JP 3136902B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- carrier
- anaerobic
- aerobic
- anaerobic 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.)
- 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
- Biological Treatment Of Waste Water (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、廃水処理に使用する嫌
気槽および好気槽の容積を小さくできる汚水の処理方法
に関するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating wastewater which can reduce the volume of an anaerobic tank and an aerobic tank used for wastewater treatment.
【０００２】[0002]
【従来の技術】従来、汚水から生物学的に窒素成分を除
去する方法として活性汚泥循環変法があり、リン成分を
除去する方法として嫌気無酸素好気法がある。この方法
は、リン成分を吐き出させる嫌気槽（前処理槽）、窒素
成分を主に除去する嫌気槽（以降、脱窒槽という）、好
気槽および最終沈殿池を設け、嫌気槽に最終沈澱池から
の返送汚泥と流入汚水を導入し、嫌気状態で活性汚泥か
らリン成分を吐き出させる。脱窒槽には嫌気槽流出活性
汚泥混合液と好気槽処理水の一部を導入し、脱窒槽で脱
窒菌の作用により硝酸性窒素（ＮＯ3 −Ｎともいう）を
窒素ガスに還元し、汚水から窒素成分の除去を行う。次
に、脱窒槽で処理された活性汚泥混合液は好気槽に送ら
れ、好気的条件下で硝化菌の作用によりアンモニア性窒
素（ＮＨ4−Ｎともいう）がＮＯ3 −Ｎに酸化される。
また、好気槽では前処理槽でリン成分を吐き出した量以
上のリン成分を微生物体内に取り込むので、廃水のリン
濃度は低下する。2. Description of the Related Art Conventionally, there is a modified activated sludge circulation method as a method for biologically removing nitrogen components from wastewater, and an anaerobic anoxic aerobic method as a method for removing phosphorus components. According to this method, an anaerobic tank (pretreatment tank) for discharging phosphorus components, an anaerobic tank for mainly removing nitrogen components (hereinafter referred to as a denitrification tank), an aerobic tank and a final sedimentation tank are provided. Introduces the return sludge and inflow sewage from the plant, and discharges the phosphorus component from the activated sludge under anaerobic condition. Into the denitrification tank, a mixture of the activated sludge discharged from the anaerobic tank and a part of the treatment water in the aerobic tank are introduced, and in the denitrification tank, nitrate nitrogen (NO 3 -N) is reduced to nitrogen gas by the action of denitrifying bacteria. Remove nitrogen components from sewage. Next, the activated sludge mixed solution treated in the denitrification tank is sent to the aerobic tank, and under the aerobic conditions, the ammonia nitrogen (also called NH 4 —N) is oxidized to NO 3 —N by the action of nitrifying bacteria. Is done.
Further, in the aerobic tank, the amount of phosphorus component that has been discharged from the pretreatment tank is greater than the amount of phosphorus component discharged into the microorganisms, so that the phosphorus concentration in the wastewater decreases.
【０００３】好気槽で処理された活性汚泥混合液の一部
は前述のように脱窒槽に循環され、残りは最終沈澱池に
流入し、活性汚泥と処理水の沈降分離が行われる。この
ようにして得られた上澄液は放流される。一方、沈降分
離されたリン成分を過剰に取り込んだ微生物を含む活性
汚泥の一部は、余剰汚泥として系外に引き抜かれ、別途
処分され、残りは返送汚泥として前処理槽または脱窒槽
に導入される。A part of the activated sludge mixed solution treated in the aerobic tank is circulated to the denitrification tank as described above, and the rest flows into the final settling basin, where the activated sludge and the treated water are settled and separated. The supernatant obtained in this way is discharged. On the other hand, part of the activated sludge containing microorganisms that excessively sedimented and separated phosphorus components is drawn out of the system as surplus sludge, disposed separately, and the rest is returned to the pretreatment tank or denitrification tank as sludge. You.
【０００４】上記の処理過程で、脱窒のための水素供与
体として汚水中のＢＯＤ成分の一部が利用され、除去さ
れるが、汚水中のＢＯＤの大部分は好気槽内で分解除去
される。[0004] In the above process, a part of the BOD component in the wastewater is used and removed as a hydrogen donor for denitrification, but most of the BOD in the wastewater is decomposed and removed in an aerobic tank. Is done.
【０００５】しかし、上述の方法でも、活性汚泥の脱窒
速度および硝化速度が小さく 反応槽を大型にせざるを
えない問題があった。この問題を解決するために脱窒槽
や好気槽等の反応槽に担体を存在させ、脱窒菌や硝化菌
を高濃度に反応槽内に保持し反応槽を小型化する技術が
文献−「建設省；バイオテクノロジーを活用した新排水
処理システム開発報告書（下水道編）」ｐ．６３２（１
９９１）−に記載されている。この方法は、嫌気処理を
行う前処理槽３０、脱窒槽３１、好気槽３２および沈澱
池３３を直列に配設し、廃水を順に流す廃水処理フロー
において、脱窒槽３１および好気槽３２に微生物固定化
担体３１ａ，３１ｂを投入して脱窒菌、硝化菌の高濃度
化を図っている。However, even the above-mentioned method has a problem that the denitrification rate and the nitrification rate of the activated sludge are small and the reaction tank must be large. In order to solve this problem, there is a technology in which a carrier is present in a reaction tank such as a denitrification tank or an aerobic tank, and a denitrification bacterium or a nitrifying bacterium is held at a high concentration in the reaction tank to reduce the size of the reaction tank. Ministry; Development Report of New Wastewater Treatment System Utilizing Biotechnology (Sewerage Edition) "p. 632 (1
991)-. In this method, a pretreatment tank 30 for performing anaerobic treatment, a denitrification tank 31, an aerobic tank 32, and a sedimentation basin 33 are arranged in series, and in a wastewater treatment flow in which wastewater flows sequentially, the denitrification tank 31 and the aerobic tank 32 are provided. The microorganism-immobilized carriers 31a and 31b are charged to increase the concentration of denitrifying bacteria and nitrifying bacteria.
【０００６】[0006]
【発明が解決しようとする課題】上記文献技術のように
担体（微生物固定化担体）を利用しても、脱窒槽につい
ては担体が常時嫌気状態下におかれるため、微生物の増
殖速度が小さくなり、脱窒槽の容積を小さくできないと
いう問題がある。Even if a carrier (microorganism-immobilized carrier) is used as in the above-mentioned literature technology, the denitrification tank is always placed in an anaerobic state, so that the growth rate of microorganisms is reduced. However, there is a problem that the volume of the denitrification tank cannot be reduced.
【０００７】また、文献の方法は好気槽において、脱窒
槽で脱窒のために廃水中のＢＯＤの一部が消費されるの
みで、大部分のＢＯＤが好気槽に流入し好気槽内で分
解、除去される。このため、好気槽内の担体表面では硝
化反応とＢＯＤ除去反応が同時に進行し、担体の表面は
硝化菌とＢＯＤ分解菌が共生した生物相となっている。
従って、流入汚水の負荷変動により好気槽に大量のＢＯ
Ｄが流入する場合には、担体に固定化されたＢＯＤ分解
菌が大量の酸素を消費し、硝化菌が酸素を利用出来なく
なり、硝化が阻害されるという問題がある。In the method described in the literature, in the aerobic tank, only a part of the BOD in the wastewater is consumed for denitrification in the denitrification tank, and most of the BOD flows into the aerobic tank and flows into the aerobic tank. Decomposed and removed within. Therefore, the nitrification reaction and the BOD removal reaction proceed simultaneously on the surface of the carrier in the aerobic tank, and the surface of the carrier is a biota in which nitrifying bacteria and BOD degrading bacteria coexist.
Therefore, a large amount of BO is stored in the aerobic tank due to the load fluctuation of the inflow sewage.
When D flows in, the BOD-degrading bacteria immobilized on the carrier consume a large amount of oxygen, and the nitrifying bacteria cannot use oxygen, which causes a problem that nitrification is inhibited.
【０００８】本発明は、上記の問題点を解決し、好気槽
および嫌気槽の大幅な小型化を可能とし、負荷変動に対
して安定した硝化および脱窒を行う方法を提供すること
を目的とする。An object of the present invention is to solve the above-mentioned problems, to provide a method for enabling aerobic tanks and anaerobic tanks to be significantly reduced in size, and for performing nitrification and denitrification stably with respect to load fluctuations. And
【０００９】[0009]
【課題を解決するための手段】本発明は上記の目的を、
有機性汚水を活性汚泥と微生物固定化担体により生物学
的に処理する方法において、窒素成分を除去する嫌気
槽、アンモニア成分を酸化する第１の好気槽および処理
水と活性汚泥を分離する分離手段を直列に配設し、活性
汚泥および処理水の一部と汚水を前記嫌気槽に流入させ
るとともに、前記嫌気槽および前記第１の好気槽に微生
物固定化担体を装入する一方、前記嫌気槽の槽内処理水
の一部を微生物固定化担体とともに第２の好気槽と前記
嫌気槽の間で循環させることを特徴とする汚水の処理方
法によって解決する。SUMMARY OF THE INVENTION The present invention provides the above object,
In a method of biologically treating organic wastewater with activated sludge and a microorganism-immobilized carrier, an anaerobic tank for removing nitrogen components, a first aerobic tank for oxidizing ammonia components, and separation for separating treated water from activated sludge Means are arranged in series, and a part of the activated sludge and the treated water and the sewage flow into the anaerobic tank, while loading the microorganism-immobilized carrier into the anaerobic tank and the first aerobic tank, The problem is solved by a sewage treatment method characterized by circulating a part of treated water in an anaerobic tank together with a microorganism-immobilized carrier between a second aerobic tank and the anaerobic tank.
【００１０】上記方法において、第２の好気槽と前記嫌
気槽の間での処理水および微生物固定化担体の循環量を
汚水の汚濁負荷に応じて変化させると、安定した窒素除
去が可能となる。[0010] In the above method, if the circulating amount of the treated water and the microorganism-immobilized carrier between the second aerobic tank and the anaerobic tank is changed according to the pollutant load of the sewage, stable nitrogen removal becomes possible. Become.
【００１１】[0011]
【作用】嫌気槽の担体（以下、担体Ｂという）一部は槽
内液の一部と共に第２の好気槽に流入し、ここで曝気さ
れた後、再び嫌気槽に戻される。ところで、脱窒能力を
有する細菌（脱窒菌）の種類は多く、その多くは通性嫌
気性菌と呼ばれる細菌であり、この細菌は嫌気性条件で
も、好気性条件でも生活でき、好気状態での増殖速度
は、嫌気状態での増殖速度に比べ２〜３倍大きい。この
ため、従来法の嫌気槽に担体を装入しても、担体は常時
嫌気的条件下におかれるので担体への細菌固定化量は少
なく、担体の装入効果は小さい。本発明方法において
は、嫌気槽の担体Ｂの一部は、嫌気槽と第２の好気槽の
間を循環し、担体Ｂの脱窒菌は好気性条件に曝され増殖
し、担体Ｂに大量の脱窒菌が固定され、嫌気槽に戻る。
嫌気槽内の脱窒菌濃度が上がり、従って、嫌気槽の小型
化が可能となる。即ち、嫌気槽の小型化が可能となる。A part of the carrier in the anaerobic tank (hereinafter, referred to as carrier B) flows into the second aerobic tank together with a part of the liquid in the tank, is aerated here, and is returned to the anaerobic tank again. By the way, there are many types of bacteria having a denitrifying ability (denitrifying bacteria), and most of them are bacteria called facultative anaerobic bacteria. These bacteria can live under anaerobic conditions or aerobic conditions, and can live under aerobic conditions. Is 2-3 times higher than the growth rate in an anaerobic state. For this reason, even if the carrier is loaded into the anaerobic tank of the conventional method, the carrier is always kept under anaerobic conditions, so that the amount of bacteria immobilized on the carrier is small and the loading effect of the carrier is small. In the method of the present invention, a part of the carrier B in the anaerobic tank circulates between the anaerobic tank and the second aerobic tank, and the denitrifying bacteria of the carrier B are exposed to the aerobic condition and proliferate, and the carrier B The denitrifying bacteria are fixed and return to the anaerobic tank.
The concentration of the denitrifying bacteria in the anaerobic tank increases, so that the size of the anaerobic tank can be reduced. That is, the size of the anaerobic tank can be reduced.
【００１２】また、第１の好気槽の担体（以下、担体Ａ
という）はその槽内に保持される。嫌気槽では脱窒のた
めに僅かの量のＢＯＤが分解されるが、大部分のＢＯＤ
は第１の好気槽に流入する。硝化菌は、酸素の存在下で
増殖する細菌であり、担体Ａには活性の高い硝化菌が高
濃度に固定する。これにより、第１の好気槽の小型化が
可能となる。Further, the carrier of the first aerobic tank (hereinafter, carrier A)
Is held in the tank. In the anaerobic tank, a small amount of BOD is decomposed due to denitrification.
Flows into the first aerobic tank. Nitrifying bacteria are bacteria that grow in the presence of oxygen. Nitrifying bacteria having high activity are immobilized on carrier A at a high concentration. Thereby, the size of the first aerobic tank can be reduced.
【００１３】また、第２の好気槽と前記嫌気槽の間での
処理水および微生物固定化担体の循環量を汚水の汚濁負
荷に応じて変化させるようにすると、流入水の負荷が増
加して、反応槽に大量のＢＯＤが流入しても、好気的条
件下でＢＯＤの除去速度が大きいので、嫌気槽から第２
の好気槽への循環量を増やすことによりＢＯＤが除去量
が増大し、その結果、第１の好気槽の硝化菌に常に充分
な酸素が供給されるので、安定した窒素除去が可能とな
る。Further, if the circulating amount of the treated water and the microorganism-immobilized carrier between the second aerobic tank and the anaerobic tank is changed according to the pollution load of the sewage, the load of the inflow water increases. Therefore, even if a large amount of BOD flows into the reaction tank, the BOD removal rate is high under aerobic conditions.
The amount of BOD to be removed is increased by increasing the amount of BOD circulated to the aerobic tank, and as a result, sufficient oxygen is always supplied to the nitrifying bacteria in the first aerobic tank, thus enabling stable nitrogen removal. Become.
【００１４】[0014]
【実施例】本発明の実施例を図面に基づいて以下に説明
する。図１は、本発明の処理方法の説明図である。図に
おいて、１は嫌気槽、２は、第１の好気槽、３は、最終
沈澱池である。原廃水（または、汚水）５は、嫌気槽１
に流入する。嫌気槽１の送液の中には主に通性嫌気性菌
からなる細菌を固定化する担体Ｂ（９）を、約２０％の
充填率で存在させている。嫌気槽１の槽液の出口には、
担体Ｂの第１の好気槽２への流出を防止するスクリーン
６が設けられている。嫌気槽１の担体Ｂを含む槽液の一
部は、循環ボンプ７により、第２の好気槽４に送給され
る。第２の好気槽４の槽液は、ブロワー４ａにより槽底
部の散気装置４ｂを介して曝気されている。ここで、曝
気され、細菌が増殖し、槽液のＢＯＤの一部が除去され
る。一定時間滞留した担体Ｂを含んだ槽液は嫌気槽４に
再び流入する。循環する液量は、原廃水の汚濁負荷に応
じて増減される。８は攪拌機で、嫌気槽１の槽液を攪拌
しており、ここで無酸素的攪拌状態下で主に担体Ｂに結
合された固定化細菌の作用により脱窒処理が行われる。
なお、この嫌気槽１には、最終沈澱池３の返送汚泥およ
び第１の好気槽２の上澄液（または、処理水）の一部が
流入している。DESCRIPTION OF THE PREFERRED EMBODIMENTS Embodiments of the present invention will be described below with reference to the drawings. FIG. 1 is an explanatory diagram of the processing method of the present invention. In the figure, 1 is an anaerobic tank, 2 is a first aerobic tank, and 3 is a final sedimentation basin. Raw wastewater (or sewage) 5 is anaerobic tank 1
Flows into. A carrier B (9) for immobilizing bacteria mainly composed of facultative anaerobic bacteria is present in the anaerobic tank 1 at a filling rate of about 20%. At the outlet of the tank liquid in the anaerobic tank 1,
A screen 6 for preventing the carrier B from flowing into the first aerobic tank 2 is provided. A part of the tank liquid containing the carrier B in the anaerobic tank 1 is supplied to the second aerobic tank 4 by the circulation pump 7. The bath liquid in the second aerobic tank 4 is aerated by a blower 4a via a diffuser 4b at the bottom of the tank. Here, aeration is performed, bacteria grow, and a part of the BOD in the bath liquid is removed. The tank solution containing the carrier B that has stayed for a certain time flows into the anaerobic tank 4 again. The amount of the circulating liquid is increased or decreased according to the pollution load of the raw wastewater. Reference numeral 8 denotes a stirrer, which stirs the tank liquid in the anaerobic tank 1, where the denitrification treatment is performed mainly by the action of immobilized bacteria bound to the carrier B under anoxic stirring.
The sludge returned from the final sedimentation basin 3 and a part of the supernatant (or treated water) of the first aerobic tank 2 flow into the anaerobic tank 1.
【００１５】嫌気槽１および第２の好気槽４で処理され
て、脱窒およびＢＯＤの一部除去が行われた上澄液は、
スクリーン６で担体Ｂを分離され、第１の好気槽２に流
入する。第１の好気槽２の槽底部には散気装置２ｂが設
けられており、槽液はブロワー２ａにより散気装置２ｂ
を介して曝気されている。この槽には、硝化菌を固定化
する担体Ａ（１０）を約２０％の充填率で存在させてい
る。ここで、残存するＢＯＤの除去とアンモニア性窒素
を酸化して硝酸性窒素にし、活性汚泥によるリン成分の
取込みが行われる。この際、担体Ａ（１０）に大量の硝
化菌が固定化される。また、この槽には嫌気槽１と同様
その出口に担体Ａ（１０）を分離するスクリーン１１が
設けられている。The supernatant treated in the anaerobic tank 1 and the second aerobic tank 4 and subjected to denitrification and partial removal of BOD is
The carrier B is separated by the screen 6 and flows into the first aerobic tank 2. An air diffuser 2b is provided at the bottom of the first aerobic tank 2, and the tank liquid is blown by a blower 2a.
Has been aerated. In this tank, a carrier A (10) for immobilizing nitrifying bacteria is present at a filling rate of about 20%. Here, the remaining BOD is removed, the ammonia nitrogen is oxidized to nitrate nitrogen, and the phosphorus component is taken in by activated sludge. At this time, a large amount of nitrifying bacteria is immobilized on the carrier A (10). In addition, a screen 11 for separating the carrier A (10) is provided at the outlet of this tank, similarly to the anaerobic tank 1.
【００１６】第１の好気槽２で処理され、スクリーン１
１で担体Ａ（１０）を分離された処理水は、最終沈澱池
３に流入する。ここで、処理水３ａと活性汚泥３ｂは分
離され、沈澱した活性汚泥３ｂはポンプ１３により沈澱
池３の底部より抜かれる。この活性汚泥は、一部は余剰
汚泥３ｂ2 として系外に排出され、別途処理され、残り
は返送汚泥３ｂ1 として嫌気槽１に返送される。第１の
好気槽２の処理水の一部（硝化循環液）は、ポンプ１２
により嫌気槽１に送給される。Processed in the first aerobic tank 2, the screen 1
The treated water from which the carrier A (10) has been separated in 1 flows into the final settling basin 3. Here, the treated water 3a and the activated sludge 3b are separated, and the precipitated activated sludge 3b is withdrawn from the bottom of the sedimentation basin 3 by the pump 13. The activated sludge is partly discharged out of the system as excess sludge 3b 2, it is separately treated, the remainder is returned to the anaerobic tank 1 as return sludge 3b 1. Part of the treated water (nitrification circulating liquid) in the first aerobic tank 2 is supplied to a pump 12
To the anaerobic tank 1.
【００１７】本発明に使用する担体Ａ（１０）および担
体Ｂ（９）は、微生物を固定化できるもので、粒状で水
中で流動するものであれば、種々のものが使用できる。
その例としては、ポリエチレングリコールやポリプロピ
レングリコール、ポリビニルアルコールあるいはアクリ
ルアミドのような水溶性高分子の単独あるいは混合物を
ゲル化したもの、前記水溶性高分子に微生物を混合しゲ
ル化した包括固定化担体、砂、活性炭、プラスチック、
スポンジ状の粒子または小片、さらには、微生物固定化
用として市販されている担体がある。なお、担体Ｂ
（９）としては、球状、立方体、直方体や円柱状のもの
よりストローを短く切断した円筒状のものが好ましい。
また、嫌気槽１の槽液は攪拌機で攪拌しているが、酸素
を水中に巻き込まない水中攪拌機等を使用することが好
ましい。嫌気槽１の攪拌の方法としては、嫌気槽１の上
部に蓋をして密閉し、上部空間の気体を槽底部から吹込
み、槽液を攪拌する方法がある。As the carrier A (10) and the carrier B (9) used in the present invention, various carriers can be used as long as they can immobilize microorganisms and are granular and flow in water.
Examples thereof include those obtained by gelling a single or mixture of water-soluble polymers such as polyethylene glycol and polypropylene glycol, polyvinyl alcohol and acrylamide, entrapping immobilization carriers obtained by mixing microorganisms with the water-soluble polymers and gelling, Sand, activated carbon, plastic,
There are sponge-like particles or small pieces, as well as carriers that are commercially available for immobilizing microorganisms. The carrier B
As (9), a cylindrical shape obtained by cutting a straw shorter than a spherical, cubic, rectangular parallelepiped or cylindrical shape is preferable.
Further, although the tank liquid in the anaerobic tank 1 is stirred by a stirrer, it is preferable to use a submerged stirrer or the like which does not involve oxygen in water. As a method of stirring the anaerobic tank 1, there is a method in which the upper part of the anaerobic tank 1 is closed and sealed, gas in the upper space is blown from the bottom of the tank, and the tank liquid is stirred.
【００１８】上述の実施例では、第１の好気槽２から流
出した活性汚泥の混合した処理水を沈澱池で処理水と活
性汚泥に分離しているが、この分離には、沈澱池に代え
て遠心分離、加圧浮上分離や膜分離等を適用することが
できる。In the above-described embodiment, the treated water mixed with the activated sludge flowing out of the first aerobic tank 2 is separated into the treated water and the activated sludge in the sedimentation basin. Instead, centrifugation, pressure flotation, membrane separation, or the like can be applied.
【００１９】図２は、図１の流動性の担体Ａ（１０）の
代わりに、槽に固定できるハニカム状あるいは紐状の担
体Ａ' （１４）を使用している例を示す。この例の場合
は、担体Ａ' が槽に固定されているので担体の分離手段
であるスクリーン１１は不要となる。FIG. 2 shows an example in which a honeycomb-shaped or string-shaped carrier A '(14) which can be fixed to a tank is used in place of the fluid carrier A (10) of FIG. In this case, since the carrier A 'is fixed to the tank, the screen 11 as the carrier separating means is not required.
【００２０】図３は、図１の嫌気槽１の上流に（手前
に）嫌気性条件で原廃水を処理する前処理槽２０を設け
て、この槽に原廃水５および返送汚泥３ｂ1 を入れるよ
うにしている。この槽は槽液を攪拌機２１で攪拌してお
り、槽内では装入された返送汚泥即ち活性汚泥からリン
成分の吐き出しが行われる。この槽からの流出液は嫌気
槽１に流入する。嫌気槽１以降の処理は、図１の内容と
同一である。[0020] Figure 3 (forward) upstream of the anaerobic tank 1 of Figure 1 provided with a pretreatment reservoir 20 for processing the raw waste water under anaerobic conditions, add the raw waste water 5 and return sludge 3b 1 in this tank Like that. In this tank, the tank liquid is stirred by the stirrer 21, and in the tank, the phosphorus component is discharged from the returned sludge, that is, the activated sludge. The effluent from this tank flows into the anaerobic tank 1. The processes after the anaerobic tank 1 are the same as those in FIG.
【００２１】図４は、図３の流動性の担体Ａ（１０）の
代わりに、槽に固定できるハニカム状あるいは紐状の担
体Ａ' （１４）を使用している例を示す。この例の場合
は、担体Ａ' が槽に固定されているので担体の分離手段
であるスクリーン１１は不要となることは図２と同様で
ある。FIG. 4 shows an example in which a honeycomb-shaped or string-shaped carrier A '(14) which can be fixed to a tank is used in place of the fluid carrier A (10) of FIG. In the case of this example, since the carrier A 'is fixed to the tank, the screen 11 which is a means for separating the carrier is not required as in FIG.
【００２２】次に、図１の処理フローで原廃水を処理し
た実験結果（実施例１という）、図２の処理フローで原
廃水を処理した実験結果（実施例２という）および図６
のフローで原廃水を処理した実験結果（従来例という）
表１に示す。Next, the results of an experiment in which raw wastewater was treated according to the processing flow of FIG. 1 (referred to as Example 1), the results of an experiment in which raw wastewater was treated according to the processing flow of FIG. 2 (referred to as Example 2), and FIGS.
Result of treating raw wastewater with the flow shown in Fig. (Conventional example)
It is shown in Table 1.
【００２３】実験は実施例１、実施例２および従来例に
ついて表１に記載した仕様の各実験装置を並列して配置
し、これらに同一流量の原廃水を流して行った。各実験
装置で使用した担体は次の通りである。The experiments were carried out by arranging the experimental devices having specifications shown in Table 1 in parallel with those of Example 1, Example 2, and the conventional example, and supplying the same flow rate of raw wastewater to them. The carriers used in each experimental device are as follows.
【００２４】実施例１ 担体Ｂ： 外径4mm ×内径3mm ×長さ5mm ；比重 1.01 ストロー状
ポリプロピレン 担体Ａ： 外径4mm ×内径3mm ×長さ5mm ；比重 1.01 ストロー状
ポリプロピレン実施例２ 担体Ｂ： 外径4mm ×内径3mm ×長さ5mm ；比重 1.01 ストロー状
ポリプロピレン 担体Ａ：市販の紐状担体従来例 担体Ｂおよび担体Ａは実施例１と同一のもの Example 1 Carrier B: Outer diameter 4 mm x inner diameter 3 mm x length 5 mm; specific gravity 1.01 straw-shaped polypropylene Carrier A: outer diameter 4 mm x inner diameter 3 mm x length 5 mm; specific gravity 1.01 straw-shaped polypropylene Example 2 Carrier B: Outer diameter 4mm x inner diameter 3mm x length 5mm; specific gravity 1.01 Straw-like polypropylene Carrier A: Commercially available cord-like carrier Conventional carrier B and carrier A are the same as in Example 1.
【００２５】[0025]
【表１】 [Table 1]
【００２６】表１から分かるように、本発明法１および
２は従来法と比較して合計反応槽容積が３６％小さくて
よく、処理水の全窒素濃度も大幅に改善されている。こ
れは、嫌気槽内部での浮遊汚泥と担体付着汚泥の合計量
が、従来法では３２００mg/Lであるのに対し実施例１で
４５００mg/L、実施例２で４４００mg/Lと本発明法の汚
泥合計量が大幅に増加しているからである。As can be seen from Table 1, the methods 1 and 2 of the present invention require a total reactor volume of 36% smaller than that of the conventional method, and the total nitrogen concentration of the treated water is greatly improved. This is because the total amount of suspended sludge and carrier-attached sludge inside the anaerobic tank is 3500 mg / L in the conventional method, whereas 4500 mg / L in Example 1 and 4400 mg / L in Example 2 according to the method of the present invention. This is because the total amount of sludge has increased significantly.
【００２７】図５は、表１に示した仕様の本発明法（実
施例１）と従来法の実験装置で、原廃水の流入水量を変
化させて実験を行ったときの流入水の水質と処理水のそ
れの推移を示したグラフである。前述したように、合計
反応槽容積が従来法より３６％小さいにもかかわらず、
本発明方法は流入水量の変動に対しても、処理水の水質
が極めて安定且つ優れていることが分かる。即ち、処理
水の全窒素濃度について、従来法では平均値が９．４ｍ
ｇ／Ｌ、最大値が１７ｍｇ／Ｌであるのに対して、本発
明法では平均値が６．８ｍｇ／Ｌ、最大値が９．５ｍｇ
／Ｌであった。FIG. 5 shows the experimental results of the method of the present invention (Example 1) having the specifications shown in Table 1 and the conventional method. It is the graph which showed the transition of that of treated water. As mentioned above, despite the total reactor volume being 36% smaller than the conventional method,
It can be seen that the method of the present invention is extremely stable and excellent in the quality of the treated water even when the amount of inflow water varies. That is, the average value of the total nitrogen concentration of the treated water is 9.4 m in the conventional method.
g / L and the maximum value are 17 mg / L, whereas the average value is 6.8 mg / L and the maximum value is 9.5 mg in the method of the present invention.
/ L.
【００２８】以上のように、本発明法は反応槽容積を従
来法のそれの６４％にした場合でも、より高い窒素除去
率が得られ、また負荷変動に対しても従来法より格段に
安定した水質が得られることが示された。As described above, according to the method of the present invention, a higher nitrogen removal rate can be obtained even when the reactor volume is 64% of that of the conventional method, and the load fluctuation is much more stable than the conventional method. It was shown that the obtained water quality was obtained.
【００２９】[0029]
【発明の効果】本発明は、固定化担体を使用し嫌気槽の
担体を含んだ槽液を嫌気槽と好気槽の間に循環させるよ
うにしたので、嫌気槽の汚泥量を増加することができ、
反応槽を従来より大幅に小型化ができる。According to the present invention, the amount of sludge in the anaerobic tank is increased by using the immobilized carrier and circulating the tank liquid containing the carrier in the anaerobic tank between the anaerobic tank and the aerobic tank. Can be
The reaction tank can be made much smaller than before.
【００３０】また、嫌気槽と第２の好気槽の間の担体を
含んだ槽液の循環量を変化させることにより、負荷変動
に対しても安定した窒素除去が可能となる。Further, by changing the circulation amount of the tank liquid containing the carrier between the anaerobic tank and the second aerobic tank, it becomes possible to remove nitrogen stably even when the load changes.
【図１】本発明の処理方法の説明図である。FIG. 1 is an explanatory diagram of a processing method of the present invention.
【図２】本発明に係わる第１の好気槽に紐状担体を設け
た例を示す図である。FIG. 2 is a diagram showing an example in which a string-shaped carrier is provided in a first aerobic tank according to the present invention.
【図３】本発明に係わる嫌気槽の上流に嫌気性処理を行
う前処理槽を設けた例を示す図である。FIG. 3 is a diagram showing an example in which a pretreatment tank for performing anaerobic treatment is provided upstream of the anaerobic tank according to the present invention.
【図４】本発明に係わる図３の第１好気槽に紐状担体を
設けた例を示す図である。4 is a view showing an example in which a string-shaped carrier is provided in the first aerobic tank of FIG. 3 according to the present invention.
【図５】流入水量を変動させた場合の本発明法と従来法
の水質の推移を示すグラフである。FIG. 5 is a graph showing changes in water quality of the method of the present invention and the conventional method when the amount of inflow water is varied.
【図６】従来の処理方法の説明図である。FIG. 6 is an explanatory diagram of a conventional processing method.
１ 嫌気槽 ２ 第１の好気槽 ２ｂ 散気装置 ３ 最終沈澱池 ３ａ 処理水 ３ｂ 活性汚泥 ３ｂ1 返送汚泥 ３ｂ2 余剰汚泥 ４ 第２の好気槽 ４ｂ 散気装置 ５ 原廃水 ６ スクリーン ７ 循環ポンプ ８ 攪拌機 ９ 担体Ｂ １０ 担体Ａ １１ スクリーンDESCRIPTION OF SYMBOLS 1 Anaerobic tank 2 1st aerobic tank 2b Air diffuser 3 Final sedimentation basin 3a Treated water 3b Activated sludge 3b 1 Return sludge 3b 2 Excess sludge 4 2nd aerobic tank 4b Air diffuser 5 Raw wastewater 6 Screen 7 Circulation Pump 8 Stirrer 9 Carrier B 10 Carrier A 11 Screen
───────────────────────────────────────────────────── フロントページの続き (72)発明者 澤田 豊志 東京都千代田区丸の内一丁目１番２号 日本鋼管株式会社内 (56)参考文献 特開 平５−337494（ＪＰ，Ａ) 特開 平６−182392（ＪＰ，Ａ) 特開 平７−163994（ＪＰ，Ａ) (58)調査した分野(Int.Cl.7，ＤＢ名) C02F 3/34 101 C02F 3/30 ──────────────────────────────────────────────────続 き Continuation of the front page (72) Inventor Toshishi Sawada 1-2-1, Marunouchi, Chiyoda-ku, Tokyo Nippon Kokan Co., Ltd. (56) References JP-A-5-337494 (JP, A) JP-A-6 -182392 (JP, A) JP-A-7-163994 (JP, A) (58) Fields investigated (Int. Cl. 7 , DB name) C02F 3/34 101 C02F 3/30
Claims (2)
体により生物学的に処理する方法において、窒素成分を
除去する嫌気槽、アンモニア成分を酸化する第１の好気
槽および処理水と活性汚泥を分離する分離手段を直列に
配設し、前記嫌気槽および前記第１の好気槽に微生物固
定化担体を存在させ、前記嫌気槽の槽内処理水の一部を
微生物固定化担体とともに第２の好気槽と前記嫌気槽の
間で循環させることを特徴とする汚水の処理方法。1. A method for biologically treating organic wastewater with activated sludge and a microorganism-immobilizing carrier, wherein an anaerobic tank for removing a nitrogen component, a first aerobic tank for oxidizing an ammonia component, and treated water Separating means for separating sludge is disposed in series, a microorganism-immobilized carrier is present in the anaerobic tank and the first aerobic tank, and a part of the treatment water in the anaerobic tank is treated together with the microorganism-immobilized carrier. A method for treating wastewater, wherein the wastewater is circulated between a second aerobic tank and the anaerobic tank.
前記嫌気槽の間での処理水および微生物固定化担体の循
環量を汚水の汚濁負荷に応じて変化させる汚水の処理方
法。2. The method for treating sewage according to claim 1, wherein the circulation amount of the treated water and the microorganism-immobilized carrier between the second aerobic tank and the anaerobic tank is changed according to the pollutant load of the sewage.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11577994A JP3136902B2 (en) | 1994-05-30 | 1994-05-30 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11577994A JP3136902B2 (en) | 1994-05-30 | 1994-05-30 | Wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH07313992A JPH07313992A (en) | 1995-12-05 |
| JP3136902B2 true JP3136902B2 (en) | 2001-02-19 |
Family
ID=14670856
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| JP11577994A Expired - Fee Related JP3136902B2 (en) | 1994-05-30 | 1994-05-30 | Wastewater treatment method |
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| Country | Link |
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| JP (1) | JP3136902B2 (en) |
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| JP5053911B2 (en) * | 2008-04-07 | 2012-10-24 | 大栄産業株式会社 | Septic tank |
| JP5062572B2 (en) * | 2008-07-01 | 2012-10-31 | 新日本フエザーコア株式会社 | Contact oxidation combination system |
| JP5306296B2 (en) * | 2010-08-09 | 2013-10-02 | 株式会社日立製作所 | Waste water treatment apparatus and waste water treatment method |
| JP2013236996A (en) * | 2012-05-14 | 2013-11-28 | Hitachi Ltd | Water treatment process |
| JP5951533B2 (en) * | 2013-03-13 | 2016-07-13 | 株式会社東芝 | Method and apparatus for recovering phosphorus from waste water containing phosphorus |
| JP6245744B2 (en) * | 2013-12-17 | 2017-12-13 | 学校法人 東洋大学 | Waste water treatment equipment |
| CN105084672B (en) * | 2015-08-22 | 2017-09-22 | 哈尔滨金大环境工程有限公司 | Subsection water inflow A/O composite sewage treatment equipments and sewage water treatment method |
| JP6832685B2 (en) * | 2016-11-21 | 2021-02-24 | 株式会社クラレ | Treatment method of nitrogen-containing wastewater |
| CN109485153A (en) * | 2018-12-19 | 2019-03-19 | 清华-伯克利深圳学院筹备办公室 | A kind of biofilm reactor and method of wastewater efficient denitrogenation |
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