JP3797554B2 - Organic wastewater treatment method and equipment - Google Patents
Organic wastewater treatment method and equipment Download PDFInfo
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- JP3797554B2 JP3797554B2 JP2002313771A JP2002313771A JP3797554B2 JP 3797554 B2 JP3797554 B2 JP 3797554B2 JP 2002313771 A JP2002313771 A JP 2002313771A JP 2002313771 A JP2002313771 A JP 2002313771A JP 3797554 B2 JP3797554 B2 JP 3797554B2
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- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
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- 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
Description
【０００１】
【発明の属する技術分野】
本発明は、溶解性有機物を有した排水の処理に係り、特に、下水、排水等の溶解性有機性排水を生物学的に処理する有機性排水の処理方法と装置に関する。
【０００２】
【従来の技術】
【非特許文献１】
「水処理工学」−理論と応用−、Ｐ２０４〜２０７（井出哲夫編著、技報堂出版株式会社）
有機性排水を浄化する処理方法で、発生汚泥を嫌気性消化処理する場合、従来の処理フローは図２の通りであり、最初沈殿池での発生汚泥と最終沈殿池での余剰汚泥とのいずれか、あるいは両方を、嫌気性消化処理する。この場合、原水中の溶解性有機物は、生物反応槽において酸化反応と微生物合成反応とによって、炭酸ガスと水と生物細胞に変化する。
最初沈殿池での発生汚泥は、原水中の比較的沈降速度の大きい固形物であり、原水中の溶解性有機物の除去には関与していない。一方、最終沈殿池で発生する汚泥の多くは、微生物合成反応によって生じた生物細胞である。即ち、原水に含まれている溶解性有機物は、生物反応槽で炭酸ガスと水と生物細胞とになり、生物細胞となった分のみが嫌気性消化処理の対象となる。
【０００３】
この処理方法では、次のような問題がある。
▲１▼原水に含まれる溶解性有機物は、嫌気性消化処理で可燃性ガスとして回収される割合が低い。これは、溶解性有機物が、生物反応槽で炭酸ガスと水と生物細胞に変換され、生物細胞となった分のみが嫌気性消化処理に供され、嫌気性消化処理で分解した生物細胞のみが、可燃性ガスとして回収されるという反応を経るためである。
▲２▼活性汚泥によって溶解性有機物を処理するため、最終沈殿池からの汚泥返送設備が必要である。
▲３▼生物反応槽の負荷を増大させるためには、ＭＬＳＳ濃度を大きくすることが有効であるが、ＭＬＳＳの増加は沈殿池の増大を伴う。一般的なＭＬＳＳ濃度である２，０００〜３，０００ｍｇ／Ｌを維持して、溶解性有機物除去量を大きくするには、生物反応槽容量を大きくする必要がある。このため敷地面積が大きくなる。
▲４▼最終沈殿池での固液分離処理水のＳＳ濃度は、通常１０ｍｇ／Ｌ前後であるため、処理水を再利用するには、砂ろ過処理によるＳＳ濃度の低減が必要である。
【０００４】
【発明が解決しようとする課題】
本発明は、上記従来技術の問題点を解消し、溶解性有機物を生物細胞に変換せずに嫌気性消化処理へ供することにより、可燃性ガスの回収率を向上し、設備設置面積の狭い有機性排水の処理方法と装置を提供することを課題とする。
【０００５】
【課題を解決するための手段】
上記課題を解決するために、本発明では、溶解性有機物を含有する排水を、曝気工程、固液分離工程及び好気性ろ過工程で順次浄化する処理方法において、前記曝気工程では、ＢＯＤ酸化菌を保持する担体の存在下で、該担体あたりのＢＯＤ負荷を２０〜７０ｋｇ／（ｍ 3 担体・日）として処理し、該処理後の排水を固液分離工程で固液分離した後、該分離水を好気性ろ過工程で好気性ろ床法で処理すると共に、該分離汚泥を嫌気性消化工程で処理し、前記好気性ろ過工程の逆洗排水を前記固液分離工程あるいは曝気工程に返送して処理することを特徴とする有機性排水の処理方法としたものである。
前記処理方法において、固液分離工程には、凝集剤を添加することができる。
【０００６】
また、本発明では、溶解性有機物を含有する排水を順次処理する曝気槽、固液分離槽及び好気性ろ過槽を直列に組合わせた処理装置において、前記曝気槽が、ＢＯＤ酸化菌を保持する担体を内部に有し、前記固液分離槽は、分離水を好気性ろ過槽に、分離汚泥を嫌気性消化槽に導く経路を有し、前記好気性ろ過槽が、好気性固定床型生物ろ床と該ろ床の下方に空気を散気する手段及びろ床の逆洗排水受槽を有すると共に、該逆洗排水受槽から前記固液分離槽あるいは前記曝気槽に逆洗排水を循環する経路を有することを特徴とする有機性排水の処理装置としたものである。
【０００７】
【発明の実施の形態】
本発明において、第１段は、ＢＯＤ酸化菌を保持する担体が存在する曝気槽であり、ＢＯＤ酸化菌が対数増殖期である状態を維持して処理を行う。第２段は、固液分離槽であり、引抜汚泥を嫌気性消化処理へ供する。第３段は、好気性ろ過槽であり、逆洗排水は第２段の固液分離槽あるいは第１段の曝気槽へ返送する。
ＢＯＤ酸化菌による溶解性有機物の分解反応は、まず溶解性有機物がＢＯＤ酸化菌に吸着し、次いで吸着した有機物が酸化反応と微生物合成反応とにより、炭酸ガスと水と生物細胞に変換される。
本発明では、被処理水中の溶解性有機物をＢＯＤ酸化菌に吸着させ、吸着した有機物が炭酸ガスと水と生物細胞に変換される前に、固液分離を行い嫌気性消化処理へ供する。
即ち、本発明では、原水の溶解性有機物を生物細胞へ変換してではなく、生物細胞に吸着した状態で嫌気性消化処理に供する。このため、酸化分解による有機物の損失が少なくなり、嫌気性消化処理での消化の効率が高くなり、結果として、可燃性ガスの回収率を従来法よりも高くすることができる。
【０００８】
このために、本発明では、溶解性ＢＯＤ負荷を２０〜７０ｋｇ−ＢＯＤ／（ｍ3担体・日）以上にして、曝気槽をＢＯＤ酸化菌が対数増殖期である状態に維持する。
担体を用いず、浮遊状態の活性汚泥を用いた場合、ＢＯＤ負荷を大きくすると、曝気槽内にＢＯＤ酸化菌を保持することが困難となる。特に、下水のように水質や水量の変化が大きい場合は、浮遊状態の活性汚泥の沈降特性が変化し、後段の固液分離槽で沈降できなくなり、大部分の活性汚泥が好気性ろ床へ移動し、好気性ろ床の目詰まりの原因となることが頻繁に生じる。よって、本発明における第１段の曝気槽は、ＢＯＤ酸化担体を投入して、ＢＯＤ酸化菌を曝気槽内に保持するすることが重要である。したがって、本発明では、活性汚泥付着担体を用いることが不可欠である。
【０００９】
これにより、曝気槽容量を小さくして敷地面積の縮小を行う。
この場合、ＢＯＤ酸化担体は、曝気によって自由に流動していることが望ましい。担体の流動は、担体表面の拡散をよくして、基質が担体内部まで移動することを可能とすると共に、担体表面に成長する生物膜の剥離を促して、担体同士が生物膜により固着するのを防止する役目がある。
よって、曝気槽内には、生物膜として担体表面に付着した生物細胞と、担体から剥離した浮遊性の生物細胞が混在する。担体表面に付着した生物細胞は、曝気槽内に保持される一方、担体から剥離した浮遊性の生物細胞は、曝気槽から流出して固液分離槽で回収されて嫌気性消化処理に供される。
曝気槽容積に対する担体の投入量は、曝気槽内で担体が自由に流動するために４０％以下にすることが望ましく、ＢＯＤ酸化菌を保持するために１０％以上にすることが望ましい。
【００１０】
第２段の固液分離槽は、溶解性有機物が吸着した生物細胞を回収して嫌気性消化処理へ供する工程であり、無機凝集剤あるいは高分子凝集剤を添加して回収率を高めることが可能である。
第３段の好気性ろ過槽は、第１段の曝気槽で除去しきれない溶解性有機物と、第２段の固液分離槽で除去しきれない懸濁物質とを除去するための工程である。第３段で用いる好気性ろ床法は、酸素吸収効率が高いためブロワー動力費が低くできると共に、ろ過処理を兼ねるために、処理水は清澄であり、そのままで再利用が可能である。
本発明では、ＢＯＤ酸化担体を有した曝気槽と、好気性ろ過槽を併用することによって、活性汚泥を用いる必要が無くなり、このため汚泥返送用設備が不要となる。
【００１１】
次に、本発明の有機性排水の処理装置の一例を示す図１のフロー構成図を用いて本発明を説明する。
図１において、１は内部にＢＯＤ酸化担体５が浮遊し、流出口に担体分離スクリーン６を有する曝気槽であり、２は固液分離槽であり、３は内部にろ材層７を有する好気性ろ過槽であり、４は処理水槽である。
被処理水８は、好気性ろ過槽の逆洗排水９と共に曝気槽１に流入する。曝気槽１には、担体５と共に担体から剥離した生物フロックと好気性ろ床の逆洗排水に含まれる生物フロックが浮遊しており、被処理水８に含まれる溶解性有機物は、担体５表面の生物膜及び生物フロックに吸着する。
【００１２】
曝気槽処理水と生物フロックは、スクリーン６により担体５と分離された後に、固液分離槽２へ流入する。
固液分離槽２では、溶解性有機物が吸着した生物細胞を沈降分離し、濃縮汚泥１０として嫌気性消化処理へ供する。
好気性ろ過槽３では、曝気槽１で除去しきれなかった溶解性有機物の分解を行うと共に、固液分離槽２で除去しきれなかった懸濁物質を、生物膜ろ過作用により除去し、処理水槽４を経て処理水１１として放流される。
本発明では、曝気槽処理水に凝集剤１２を添加して、固液分離槽における懸濁物質除去効率を向上することも可能である。
【００１３】
【実施例】
以下、本発明を実施例により具体的に説明する。
実施例１
図１の処理フローを用いた場合の処理性能を表１に示す。但し、本例は、好気性ろ過槽の逆洗排水を、曝気槽１へ返送した場合のものである。曝気槽の処理条件は、担体充填率＝３０％、溶解性ＢＯＤ負荷＝４０ｋｇ／（ｍ3担体・ｄ）であり、溶解性ＢＯＤの７０％は生物細胞に吸着して固液分離槽へ移行し、１０％は炭酸ガスと水と生物細胞に変換する。固液分離槽の処理条件は、ＳＳ除去率６０％である。この場合、嫌気性消化処理によるメタンガス発生量は４，０００Ｎ−ｍ3／ｄとなる。
一方、曝気槽における溶解性有機物除去率を８０％とし、除去された全量が炭酸ガスと水と生物細胞に変換した場合には、嫌気性消化処理によるメタンガス発生量は３，３００Ｎ−ｍ3／ｄである。
【００１４】
【表１】
【発明の効果】
本発明によれば、以下の効果を奏することができる。
（１）溶解性有機物を生物細胞に変換することなく嫌気性消化処理へ供することができ、嫌気性消化処理における可燃性ガスの回収率を高くすることができる。
（２）浮遊式活性汚泥を用いないため、沈殿池と汚泥返送用設備が不要である。
（３）ＢＯＤ酸化菌を担体に付着させることによって、曝気槽内に保持することができ、安定した処理が可能であると共に、曝気槽容積を小さし、装置の敷地面積を狭くすることができる。
（４）好気性ろ床法は、酸素吸収効率が高いためブロワー動力費が低くできると共に、ろ過処理を兼ねるために処理水は清澄であり、そのままで再利用が可能である。
【図面の簡単な説明】
【図１】本発明の処理装置の一例を示すフロー構成図。
【図２】従来の処理装置を示すフロー構成図。
【符号の説明】
１：曝気槽、２：固液分離槽、３：好気性ろ過槽、４：処理水槽、５：担体、６：スクリーン、７：ろ材層、８：被処理水、９：好気性ろ過槽逆洗排水、１０：濃縮汚泥、１１：処理水、１２：凝集剤[0001]
BACKGROUND OF THE INVENTION
The present invention relates to treatment of wastewater having soluble organic matter, and more particularly to a method and apparatus for treating organic wastewater that biologically treats soluble organic wastewater such as sewage and wastewater.
[0002]
[Prior art]
[Non-Patent Document 1]
"Water treatment engineering"-Theory and application-, P204-207 (edited by Tetsuo Ide, Gihodo Publishing Co., Ltd.)
When the generated sludge is anaerobically digested with a treatment method that purifies organic wastewater, the conventional treatment flow is as shown in Fig. 2. Either the generated sludge in the first sedimentation basin or the excess sludge in the final sedimentation basin Or anaerobic digestion of both. In this case, the soluble organic matter in the raw water is changed into carbon dioxide gas, water, and biological cells by the oxidation reaction and the microbial synthesis reaction in the biological reaction tank.
The sludge generated in the first sedimentation basin is a solid having a relatively high sedimentation rate in the raw water, and is not involved in the removal of soluble organic matter in the raw water. On the other hand, most of the sludge generated in the final sedimentation basin is a biological cell generated by a microbial synthesis reaction. That is, the soluble organic matter contained in the raw water becomes carbon dioxide gas, water, and biological cells in the biological reaction tank, and only the portion that has become the biological cells is subjected to anaerobic digestion treatment.
[0003]
This processing method has the following problems.
(1) Dissolved organic substances contained in raw water have a low rate of being recovered as a flammable gas by anaerobic digestion treatment. This is because dissolved organic matter is converted into carbon dioxide gas, water, and biological cells in the biological reaction tank, and only the biological cells that have been decomposed by the anaerobic digestion process are subjected to the anaerobic digestion process. This is because it undergoes a reaction of being recovered as a combustible gas.
(2) In order to treat soluble organic matter with activated sludge, a sludge return facility from the final sedimentation basin is required.
(3) In order to increase the load on the biological reaction tank, it is effective to increase the MLSS concentration, but the increase in MLSS is accompanied by an increase in the sedimentation basin. In order to maintain the general MLSS concentration of 2,000 to 3,000 mg / L and increase the amount of dissolved organic matter removed, it is necessary to increase the capacity of the biological reaction tank. This increases the site area.
(4) Since the SS concentration of the solid-liquid separation treated water in the final sedimentation basin is usually around 10 mg / L, it is necessary to reduce the SS concentration by sand filtration in order to reuse the treated water.
[0004]
[Problems to be solved by the invention]
The present invention solves the above-mentioned problems of the prior art and improves the recovery rate of combustible gas by using an organic anaerobic digestion process without converting soluble organic matter into biological cells. It is an object of the present invention to provide a method and apparatus for treating effluent.
[0005]
[Means for Solving the Problems]
In order to solve the above-mentioned problems, in the present invention, in a treatment method for sequentially purifying waste water containing soluble organic substances in an aeration process, a solid-liquid separation process and an aerobic filtration process, in the presence of a carrier for holding, after the BOD load per carrier and treated with 20~70kg / (m 3 carrier-day), and solid-liquid separation wastewater after the treatment with the solid-liquid separation step, the The separated water is treated in the aerobic filtration process in the aerobic filtration process, and the separated sludge is treated in the anaerobic digestion process, and the backwash waste water from the aerobic filtration process is returned to the solid-liquid separation process or the aeration process. It is set as the processing method of the organic waste water characterized by processing it.
In the treatment method, a flocculant can be added to the solid- liquid separation step.
[0006]
In the present invention, the aeration tank for sequentially processing the waste water containing dissolved organic matter, in the processing apparatus the solid-liquid separation tank and an aerobic filtration tank in combination in series, the aeration tank, the BOD-oxidizing bacteria retained The solid-liquid separation tank has a path for guiding the separated water to the aerobic filtration tank and the separated sludge to the anaerobic digestion tank, and the aerobic filtration tank is an aerobic fixed bed type. There is a biological filter bed and means for diffusing air below the filter bed and a backwash drainage tank for the filterbed, and backwash drainage is circulated from the backwash drainage tank to the solid-liquid separation tank or the aeration tank. The organic waste water treatment apparatus is characterized by having a route.
[0007]
DETAILED DESCRIPTION OF THE INVENTION
In the present invention, the first stage is an aeration tank in which a carrier holding BOD oxidizing bacteria is present, and the treatment is performed while maintaining the state where the BOD oxidizing bacteria are in the logarithmic growth phase. The second stage is a solid-liquid separation tank, and the extracted sludge is subjected to an anaerobic digestion treatment. The third stage is an aerobic filtration tank, and the backwash waste water is returned to the second stage solid-liquid separation tank or the first stage aeration tank.
In the decomposition reaction of the soluble organic substance by the BOD oxidizing bacteria, the soluble organic substance is first adsorbed on the BOD oxidizing bacteria, and then the adsorbed organic substance is converted into carbon dioxide gas, water, and biological cells by the oxidation reaction and the microbial synthesis reaction.
In the present invention, soluble organic substances in the water to be treated are adsorbed by BOD oxidizing bacteria, and before the adsorbed organic substances are converted into carbon dioxide gas, water, and biological cells, solid-liquid separation is performed for anaerobic digestion treatment.
That is, in this invention, it does not convert the soluble organic substance of raw | natural water into a biological cell, but uses it for the anaerobic digestion process in the state adsorb | sucked to the biological cell. For this reason, the loss of organic substances due to oxidative decomposition is reduced, the efficiency of digestion in the anaerobic digestion treatment is increased, and as a result, the recovery rate of combustible gas can be made higher than that of the conventional method.
[0008]
Therefore, in the present invention, the soluble BOD load is set to 20 to 70 kg-BOD / (m 3 carrier · day) or more, and the aeration tank is maintained in a state where the BOD oxidizing bacteria are in the logarithmic growth phase.
When floating activated sludge is used without using a carrier, it is difficult to retain BOD oxidizing bacteria in the aeration tank if the BOD load is increased. In particular, when there is a large change in water quality or water volume, such as sewage, the sedimentation characteristics of suspended activated sludge will change, making it impossible to settle in the subsequent solid-liquid separation tank, and most of the activated sludge will move to the aerobic filter bed. It often happens that it moves and causes clogging of the aerobic filter bed. Therefore, it is important for the first-stage aeration tank in the present invention to introduce the BOD oxidation carrier and hold the BOD oxidation bacteria in the aeration tank. Therefore, in the present invention, it is essential to use an activated sludge adhesion carrier.
[0009]
Thereby, the aeration tank capacity is reduced and the site area is reduced.
In this case, it is desirable that the BOD oxidation carrier flows freely by aeration. The flow of the carrier improves the diffusion on the surface of the carrier, enables the substrate to move to the inside of the carrier, promotes the peeling of the biofilm growing on the surface of the carrier, and the carriers adhere to each other by the biofilm. It has a role to prevent.
Therefore, in the aeration tank, biological cells attached to the surface of the carrier as a biological film and floating biological cells detached from the carrier are mixed. Biological cells adhering to the surface of the carrier are held in the aeration tank, while the floating biological cells detached from the carrier flow out of the aeration tank and are collected in the solid-liquid separation tank and subjected to anaerobic digestion treatment. The
The input amount of the carrier with respect to the volume of the aeration tank is desirably 40% or less for the carrier to freely flow in the aeration tank, and desirably 10% or more for retaining the BOD oxidizing bacteria.
[0010]
The second-stage solid-liquid separation tank is a process in which biological cells adsorbed with soluble organic substances are collected and subjected to anaerobic digestion treatment, and an inorganic flocculant or a polymer flocculant is added to increase the recovery rate. Is possible.
The third-stage aerobic filtration tank is a process for removing soluble organic substances that cannot be removed by the first-stage aeration tank and suspended substances that cannot be removed by the second-stage solid-liquid separation tank. is there. The aerobic filter method used in the third stage can reduce the blower power cost because of its high oxygen absorption efficiency, and the treated water is clear and can be reused as it is because it also serves as a filtration treatment.
In the present invention, the combined use of an aeration tank having a BOD oxidation carrier and an aerobic filtration tank eliminates the need for using activated sludge, and thus eliminates sludge return equipment.
[0011]
Next, the present invention will be described using the flow configuration diagram of FIG. 1 showing an example of the organic wastewater treatment apparatus of the present invention.
In FIG. 1, 1 is an aeration tank in which a BOD oxidation carrier 5 floats inside and has a carrier separation screen 6 at the outlet, 2 is a solid-liquid separation tank, and 3 is an aerobic having a
The treated water 8 flows into the aeration tank 1 together with the backwash drainage 9 of the aerobic filtration tank. In the aeration tank 1, the biological floc peeled off from the carrier together with the carrier 5 and the biological floc contained in the backwash drainage of the aerobic filter bed float, and the soluble organic matter contained in the water 8 to be treated is on the surface of the carrier 5. Adsorb to biofilms and flocs.
[0012]
The aeration tank treated water and the biological floc are separated from the carrier 5 by the screen 6 and then flow into the solid-liquid separation tank 2.
In the solid-liquid separation tank 2, biological cells adsorbed with soluble organic matter are settled and subjected to anaerobic digestion treatment as concentrated sludge 10.
In the aerobic filtration tank 3, dissolved organic substances that could not be removed in the aeration tank 1 are decomposed, and suspended substances that could not be removed in the solid-liquid separation tank 2 are removed by biofilm filtration and treated. It is discharged as treated water 11 through the water tank 4.
In the present invention, the flocculant 12 can be added to the aeration tank treated water to improve the suspended solid removal efficiency in the solid-liquid separation tank.
[0013]
【Example】
Hereinafter, the present invention will be specifically described by way of examples.
Example 1
Table 1 shows the processing performance when the processing flow of FIG. 1 is used. However, this example is a case where the backwash drainage of the aerobic filtration tank is returned to the aeration tank 1. The treatment conditions of the aeration tank are: carrier loading rate = 30%, soluble BOD load = 40 kg / (m 3 carrier · d), 70% of the soluble BOD is adsorbed on the biological cells and transferred to the solid-liquid separation tank 10% is converted into carbon dioxide gas, water and biological cells. The processing condition of the solid-liquid separation tank is an SS removal rate of 60%. In this case, the amount of methane gas generated by the anaerobic digestion process is 4,000 N-m 3 / d.
On the other hand, when the dissolved organic matter removal rate in the aeration tank is 80% and the total amount removed is converted into carbon dioxide gas, water, and biological cells, the amount of methane gas generated by anaerobic digestion is 3,300 N-m 3 / d.
[0014]
[Table 1]
【The invention's effect】
According to the present invention, the following effects can be obtained.
(1) The soluble organic matter can be subjected to an anaerobic digestion treatment without being converted into biological cells, and the recovery rate of the combustible gas in the anaerobic digestion treatment can be increased.
(2) Since floating activated sludge is not used, a sedimentation basin and sludge return equipment are not required.
(3) By attaching the BOD oxidizing bacteria to the carrier, it can be held in the aeration tank, stable treatment is possible, the aeration tank volume can be reduced, and the site area of the apparatus can be reduced. .
(4) The aerobic filter bed method can reduce the blower power cost because of its high oxygen absorption efficiency, and the treated water is clear and can be reused as it is because it serves as a filtration treatment.
[Brief description of the drawings]
FIG. 1 is a flowchart showing an example of a processing apparatus of the present invention.
FIG. 2 is a flow configuration diagram showing a conventional processing apparatus.
[Explanation of symbols]
1: aeration tank, 2: solid-liquid separation tank, 3: aerobic filtration tank, 4: treated water tank, 5: carrier, 6: screen, 7: filter medium layer, 8: treated water, 9: aerobic filtration tank reverse Wash drainage, 10: concentrated sludge, 11: treated water, 12: flocculant
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| JP2002313771A JP3797554B2 (en) | 2002-10-29 | 2002-10-29 | Organic wastewater treatment method and equipment |
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| JP2002313771A JP3797554B2 (en) | 2002-10-29 | 2002-10-29 | Organic wastewater treatment method and equipment |
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| CN106630490A (en) * | 2015-07-26 | 2017-05-10 | 李娜 | Method for removing cadmium-containing sewage pollutants |
| CN110436596A (en) * | 2019-09-05 | 2019-11-12 | 辽宁城建设计院有限公司 | A kind of processing of combined type backwashing water and reclaiming system |
| JP7017165B2 (en) * | 2020-03-31 | 2022-02-08 | 栗田工業株式会社 | Aerobic biological membrane treatment methods and equipment |
| CN111704320B (en) * | 2020-06-30 | 2022-04-22 | 桂林理工大学 | Sewage treatment system and sewage treatment method for regulating and controlling logarithmic phase growth of microorganisms |
| CN111908603A (en) * | 2020-08-21 | 2020-11-10 | 惠州市合新科技有限公司 | Novel anaerobic biological filter wastewater treatment equipment and wastewater treatment method thereof |
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