JPH11197690A - Anaerobic biological treatment method and apparatus for organic solid-containing waste water - Google Patents
Anaerobic biological treatment method and apparatus for organic solid-containing waste waterInfo
- Publication number
- JPH11197690A JPH11197690A JP1823598A JP1823598A JPH11197690A JP H11197690 A JPH11197690 A JP H11197690A JP 1823598 A JP1823598 A JP 1823598A JP 1823598 A JP1823598 A JP 1823598A JP H11197690 A JPH11197690 A JP H11197690A
- Authority
- JP
- Japan
- Prior art keywords
- reaction tank
- biological treatment
- treated water
- anaerobic
- anaerobic biological
- 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.)
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Classifications
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- Y02W10/12—
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、有機性固形物含有
廃水の嫌気性生物処理方法及び装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method and an apparatus for anaerobic biological treatment of wastewater containing organic solids.
【０００２】[0002]
【従来の技術】近年、有機物の除去技術としてメタン発
酵処理は、余剰汚泥の発生量が少なく、また、発生する
メタンガスをエネルギーとして回収できることから、処
理コストの安い技術として注目されている。メタン発酵
による有機物の分解は、酸生成菌によって有機酸を生成
する酸生成反応と、生じた有機酸をメタン生成菌によっ
てメタンガスにするメタン生成反応があり、反応槽内で
は、これらの反応が順次進行して、有機物は炭酸ガスと
メタンガスに分解されていく。特に、上向流式嫌気汚泥
床法は、嫌気性細菌を反応槽内に高濃度に保持しうるこ
とから、最も多く実用化されている。この方法では、図
２に示すように、原水を反応槽１の下部から上向流で供
給し、グラニュール（嫌気性細菌が自己造粒してできた
直径２〜３ｍｍ程度の細菌集合体）層９を通過する際に
嫌気性微生物によって有機物を分解し、メタンガスと炭
酸ガスを発生させ、処理水の一部は、原水とともに反応
槽１の下部から返送される。この処理方法は、反応槽内
にグラニュールを充填し、高有機物負荷の運転を可能に
したものである。2. Description of the Related Art In recent years, methane fermentation treatment has been attracting attention as a low-cost treatment technology because the amount of surplus sludge generated is small and the generated methane gas can be recovered as energy. The decomposition of organic matter by methane fermentation is divided into an acid production reaction that produces organic acids by acid-producing bacteria and a methane production reaction that converts the produced organic acids into methane gas by methanogens. As it progresses, organic matter is decomposed into carbon dioxide gas and methane gas. In particular, the upward flow anaerobic sludge bed method is most practically used because anaerobic bacteria can be maintained at a high concentration in a reaction tank. In this method, as shown in FIG. 2, raw water is supplied in an upward flow from the lower part of the reaction tank 1, and granules (bacteria aggregates having a diameter of about 2 to 3 mm formed by self-granulation of anaerobic bacteria) are provided. The organic matter is decomposed by the anaerobic microorganisms when passing through the layer 9 to generate methane gas and carbon dioxide gas, and a part of the treated water is returned from the lower part of the reaction tank 1 together with the raw water. In this treatment method, the reaction tank is filled with granules to enable operation with a high organic substance load.
【０００３】しかし、固形物を数百〜数千ｍｇ／Ｌ含ん
でいる原水の処理を行う場合、固形物がグラニュール表
面に付着又は捕捉され、細菌の活性低下を起こしやす
い。また、固形状有機物は、微生物分解速度が遅いた
め、反応槽内に堆積しやすい。反応槽内に堆積した固形
物は、メタンや二酸化炭素を含有する発酵ガスに同伴さ
れ、グラニュールのウォッシュアウトを引き起こすこと
がある。このため、一般に上向流式嫌気汚泥床は、固形
物濃度が数百ｍｇ／Ｌ程度の廃水を処理対象としてい
る。[0003] However, when treating raw water containing several hundred to several thousand mg / L of solids, the solids are attached or trapped on the surface of the granules, and the activity of bacteria is easily reduced. In addition, solid organic substances tend to accumulate in the reaction tank because the rate of microbial decomposition is low. Solids deposited in the reactor may be entrained in fermentation gases containing methane and carbon dioxide, causing the granules to wash out. For this reason, in general, an upward flow anaerobic sludge bed is intended for treating wastewater having a solid matter concentration of about several hundred mg / L.
【０００４】特開平４−１８０８９６号公報には、上向
流式嫌気汚泥床法を実施する反応槽の下部に酸生成菌を
担持した多孔質床を有し、その上にメタン生成菌を含む
スラッジ部を形成させ、固形物を多孔質床に捕捉させて
酸生成菌の作用を受けさせることによって、固形物の浮
上やグラニュールのウォッシュアウトを防止することが
提案されている。この方法では、固形物が酸発酵した場
合、多量の有機酸が生じ、酸発酵液のｐＨは５〜６にま
で低下し、このｐＨの低い酸発酵液がメタン発酵部に流
入することになる。しかし、メタン生成細菌の活性は、
ｐＨの影響を受けやすく、至適ｐＨ７〜８に保持する必
要があるが、ｐＨの低い酸発酵液の流入によりメタン発
酵が良好に進行しなくなってしまう。[0004] Japanese Patent Application Laid-Open No. 4-180896 discloses that a porous bed carrying acid-forming bacteria is provided at the lower part of a reaction tank in which an upflow type anaerobic sludge bed method is carried out, and methane-forming bacteria are contained thereon. It has been proposed to prevent the floating of solids and the washout of granules by forming a sludge portion, capturing solids on a porous bed and receiving the action of acid-generating bacteria. In this method, when the solid material is subjected to acid fermentation, a large amount of organic acid is generated, the pH of the acid fermentation solution is reduced to 5 to 6, and the acid fermentation solution having a low pH flows into the methane fermentation section. . However, the activity of methanogens is
It is susceptible to pH and needs to be maintained at an optimum pH of 7 to 8, but methane fermentation does not proceed well due to the inflow of an acid fermentation solution having a low pH.
【０００５】[0005]
【発明が解決しようとする課題】本発明は、前記の従来
技術の問題点を解消し、固形物濃度が高い原水の嫌気性
処理を１槽式で、グラニュールの活性低下やウォッシュ
アウトを起こすことなく効率よく実施しうる有機性固形
物含有廃水の嫌気性生物処理方法及び装置を提供するこ
とを目的とする。DISCLOSURE OF THE INVENTION The present invention solves the above-mentioned problems of the prior art, and performs anaerobic treatment of raw water having a high solids concentration in a one-tank system, causing a decrease in granule activity and a washout. An object of the present invention is to provide a method and an apparatus for anaerobic biological treatment of wastewater containing organic solid matter, which can be efficiently carried out without any problem.
【０００６】[0006]
【課題を解決するための手段】本発明は、処理水の一部
を反応槽内の生物処理部の高さ方向の途中に返送するこ
とにより反応槽内の液流速を変化させるとともに、メタ
ン発酵部の有機酸濃度を低濃度に希釈し、ｐＨの影響を
解消することによって上記課題を解決したものである。
すなわち、本発明の有機性固形物含有廃水の嫌気性生物
処理方法は、有機性固形物含有廃水を嫌気性生物反応槽
に流入させ、該反応槽内の嫌気性微生物群の作用で有機
物を分解する嫌気性生物処理方法において、処理水の一
部を、反応槽内の生物処理部の高さ方向の途中に返送
し、液流速を単一反応槽内で変化させることを特徴とす
る。また、本発明の有機性固形物含有廃水の嫌気性生物
処理装置は、有機性固形物含有廃水を嫌気性生物反応槽
に流入させ、該反応槽内の嫌気性微生物群の作用で有機
物を分解する嫌気性生物処理装置において、反応槽の最
下部に原水導入配管、反応槽頂部にガス排出口、反応槽
上部に処理水排出配管を有し、さらに処理水を貯留する
処理水槽を介して、反応槽内の生物処理部の高さ方向の
途中に処理水の一部を返送する処理水返送配管を有する
ことを特徴とする。SUMMARY OF THE INVENTION The present invention changes the liquid flow rate in a reaction tank by returning a part of the treated water to the middle of the biological treatment section in the height direction of the biological treatment section. The above-mentioned problem has been solved by diluting the organic acid concentration of a part to a low concentration to eliminate the influence of pH.
That is, the anaerobic biological treatment method of the organic solid matter-containing wastewater of the present invention comprises flowing the organic solid matter-containing wastewater into an anaerobic biological reaction tank and decomposing the organic matter by the action of anaerobic microorganisms in the reaction tank. The anaerobic biological treatment method described above is characterized in that a part of the treated water is returned halfway in the height direction of the biological treatment section in the reaction tank, and the liquid flow rate is changed in a single reaction tank. Further, the anaerobic biological treatment apparatus for organic solid matter-containing wastewater of the present invention flows organic solid matter-containing wastewater into an anaerobic biological reaction tank and decomposes organic matter by the action of anaerobic microorganisms in the reaction tank. In an anaerobic biological treatment apparatus, a raw water introduction pipe at the bottom of the reaction tank, a gas outlet at the top of the reaction tank, a treated water discharge pipe at the top of the reaction tank, and a treated water tank for storing treated water, It is characterized by having a treated water return pipe for returning part of the treated water in the height direction of the biological treatment section in the reaction tank.
【０００７】[0007]
【発明の実施の形態】本発明の方法により、処理水の一
部を、嫌気性生物反応槽内の生物処理部の高さ方向の途
中に循環水として返送すると、この循環水流入箇所の上
下で反応槽内の液流速が変化する。反応槽下部から固形
物を含む原水を通水した場合、循環水流入下部では循環
水の影響を受けず、液流速が遅いため、固形物が堆積す
る。堆積した固形物は、酸発酵が行われて有機酸とな
る。このとき、水素ガスを発生するが、水素ガスは槽上
部へ移行するため、水素分圧が上昇し、酸生成を阻害す
ることはない。一方、酸発酵された被処理水は、循環水
流入箇所より上部の生物処理部でメタン発酵され、液中
の有機酸はメタンと炭酸ガスとなる。すなわち、本発明
の方法では、循環水の流入位置より下部で酸生成が行わ
れ、それより上部でメタン発酵が行われる。DESCRIPTION OF THE PREFERRED EMBODIMENTS According to the method of the present invention, when a part of treated water is returned as circulating water in the height direction of a biological treatment section in an anaerobic biological reaction tank, the circulating water flows upward and downward. Changes the liquid flow velocity in the reaction tank. When raw water containing solids flows through the lower part of the reaction tank, solids accumulate in the lower part of the inflow of circulating water because the liquid flow velocity is slow without being affected by the circulating water. The deposited solids undergo acid fermentation to become organic acids. At this time, hydrogen gas is generated, but the hydrogen gas moves to the upper part of the tank, so that the hydrogen partial pressure increases and does not hinder acid generation. On the other hand, the treated water subjected to acid fermentation is subjected to methane fermentation in the biological treatment section above the circulating water inflow point, and the organic acids in the liquid become methane and carbon dioxide. That is, in the method of the present invention, acid is generated below the inflow position of the circulating water, and methane fermentation is performed above it.
【０００８】嫌気性生物反応槽内の生物処理部の高さ方
向の途中に処理水の一部を循環水として返送することに
より、この循環水流入位置で液は希釈され、したがって
酸発酵液の有機酸濃度も低濃度に希釈され、メタン発酵
部におけるｐＨの影響を解消する。また、処理水の循環
によりグラニュールも流動することになり、基質とグラ
ニュールの接触効率が向上し、効率のよい処理が可能に
なる。さらに、処理水にアルカリ剤を添加してから反応
槽へ返送することにより、メタン発酵部におけるｐＨの
影響をいっそう防止することができる。By returning a part of the treated water as circulating water in the height direction of the biological treatment section in the anaerobic biological reaction tank, the liquid is diluted at the circulating water inflow position, and therefore, the acid fermentation liquid The organic acid concentration is also diluted to a low concentration to eliminate the effect of pH in the methane fermentation section. In addition, the granules also flow due to the circulation of the treatment water, so that the contact efficiency between the substrate and the granules is improved, and efficient treatment is possible. Furthermore, the influence of pH in the methane fermentation section can be further prevented by returning the treated water to the reaction tank after adding an alkaline agent.
【０００９】次に、図面を参照して本発明をさらに具体
的に説明する。図１は、本発明の一実施例を示す有機性
固形物含有廃水の嫌気性生物処理装置の系統図である。
図１において、原水は、原水ポンプ２により反応槽１の
下部に流入し、原水中の固形物は、酸生成グラニュール
層３に堆積し、有機酸に分解される。生成した有機酸
は、メタン生成グラニュール層４でメタンガス及び炭酸
ガスに分解され、発生ガスはガス排出口５を通過し、系
外へ排出される。また、処理水は、処理水流出口６を通
過し、処理水槽７へ貯留される。処理水の一部は、循環
ポンプ８により反応槽の酸生成グラニュール層３とメタ
ン生成グラニュール層４の界面付近に設けられた処理水
返送口１０へ送られ、酸発酵液の希釈水として用いられ
る。Next, the present invention will be described more specifically with reference to the drawings. FIG. 1 is a system diagram of an anaerobic biological treatment apparatus for an organic solid matter-containing wastewater showing one embodiment of the present invention.
In FIG. 1, raw water flows into a lower part of a reaction tank 1 by a raw water pump 2, and solids in the raw water are deposited on an acid-generating granule layer 3 and decomposed into organic acids. The generated organic acid is decomposed into methane gas and carbon dioxide gas in the methanation granule layer 4, and the generated gas passes through the gas outlet 5 and is discharged out of the system. Further, the treated water passes through the treated water outlet 6 and is stored in the treated water tank 7. Part of the treated water is sent by a circulation pump 8 to a treated water return port 10 provided near the interface between the acid-producing granule layer 3 and the methane-producing granule layer 4 in the reaction tank, and is used as dilution water for the acid fermentation liquor. Used.
【００１０】処理水の返送の最適位置を検討するため、
図２に示す従来の上向流式嫌気汚泥床装置の循環ポンプ
８を停止し、処理水無循環型として処理を実施した。但
し、反応層内のｐＨ低下を防止するため、原水には重炭
酸ナトリウムを添加した。グラニュール層（生物処理
部）の種々の高さ位置で揮発性脂肪酸濃度を測定したと
ころ、図３に示すように、グラニュール層の最下部から
１／４〜１／３の位置までで揮発性脂肪酸濃度が著しく
増加し、この位置で酸生成菌の活性が高いことが分かっ
た。したがって、本発明において、処理水の返送口１０
を生物処理部の１／４〜１／３の位置に設けることが好
ましい。[0010] In order to examine the optimal position for returning the treated water,
The circulation pump 8 of the conventional upward flow anaerobic sludge bed apparatus shown in FIG. 2 was stopped, and the treatment was carried out as a treatment water non-circulation type. However, sodium bicarbonate was added to the raw water in order to prevent a decrease in pH in the reaction layer. When the volatile fatty acid concentration was measured at various heights of the granule layer (biological treatment section), as shown in FIG. 3, the volatile fatty acid was volatilized from 1/4 to 1/3 from the bottom of the granule layer. It was found that the concentration of the fatty acid significantly increased, and the activity of the acid-producing bacteria was high at this position. Therefore, in the present invention, the return port 10 of the treated water
Is preferably provided at a position 1/4 to 1/3 of the biological treatment section.
【００１１】また、本発明において、処理水の返送循環
量は、原水中の基質などによって適宜選択することがで
きるが、循環量が多すぎると、メタン生成グラニュール
層４における液流速がそれだけ速くなり、グラニュール
のウォッシュアウトが起こるおそれがあるので、一般
に、液流速が５ｍ／ｈ以下になるように調整するのが好
ましい。さらに、返送される処理水中のアルカリ剤も循
環され、メタン発酵に好適なｐＨ環境とすることがで
き、処理水槽内に添加されるアルカリ剤も節約すること
が可能となる。アルカリ剤の節約を考慮すると、処理水
循環量は、流入原水量の１〜１０倍とすることが好まし
い。換言すれば、処理水循環を行わない反応槽下部の液
流速と処理水循環を行う反応槽上部の液流速比率を２〜
１１の範囲とすることが好ましい。In the present invention, the amount of circulated treated water can be appropriately selected depending on the substrate in the raw water. However, if the amount of circulated water is too large, the liquid flow rate in the methane-producing granule layer 4 increases. In this case, it is generally preferable to adjust the liquid flow rate to 5 m / h or less, since there is a possibility that the granules may be washed out. Further, the alkaline agent in the returned treated water is also circulated, so that a pH environment suitable for methane fermentation can be achieved, and the alkaline agent added in the treated water tank can be saved. In consideration of saving of the alkali agent, the circulating amount of the treated water is preferably set to 1 to 10 times the amount of the inflowing raw water. In other words, the ratio of the liquid flow velocity at the lower part of the reaction tank not circulating the treated water to the liquid velocity at the upper part of the reaction tank circulating the treated water is 2 to 2.
It is preferred to be in the range of 11.
【００１２】本発明は、上向流式嫌気性汚泥床法に限定
されるものではなく、嫌気性流動床法や嫌気性固定床法
に適用することもできる。The present invention is not limited to the upward flow anaerobic sludge bed method, but can be applied to the anaerobic fluidized bed method and the anaerobic fixed bed method.
【００１３】[0013]
【実施例】次に、実施例に基づいて本発明をさらに具体
的に説明するが、本発明はこれに制限されるものではな
い。Next, the present invention will be described more specifically based on examples, but the present invention is not limited to these examples.
【００１４】実施例１ グラニュール層の高さを水面の高さの１／２とし、処理
水の返送位置をグラニュール層の１／４の位置とした本
発明の実験装置と、処理水の返送を原水と一緒に装置の
下部から行う以外は、本発明のものと同じ従来法の実験
装置とを用意した。両方の実験装置で、ＣＯＤCr５００
０ｍｇ／Ｌ、ＳＳ濃度１５００ｍｇ／Ｌの酵母含有発酵
廃水を連続的に通水し、処理実験を行った。処理水の循
環量を、両方の実験装置とも、流入原水量の２倍とし、
実験結果を図４に示す。従来法では通水量を増加させて
いくと、ＣＯＤCr容積負荷４ｋｇ／ｍ3 ・ｄの比較的低
い負荷条件においても固形物が処理水中に混入し、ＣＯ
ＤCr除去率が８０％と低い。また、通水量を増加し、Ｃ
ＯＤCr容積負荷１５ｋｇ／ｍ3 ・ｄとすると、処理水の
悪化と同時にグラニュールのウォッシュアウト現象が生
じた。一方、本発明の方法では、ＣＯＤCr容積負荷１５
ｋｇ／ｍ3 ・ｄにおいてもＣＯＤCr除去率８０％以上を
維持でき、処理水中への固形物リークも殆ど認められな
かった。Example 1 An experimental apparatus according to the present invention, in which the height of the granule layer was set to 1/2 of the height of the water surface, and the return position of the treated water was set to 1/4 of the granular layer, An experimental apparatus of the same conventional method as that of the present invention was prepared except that the return was performed from the lower part of the apparatus together with the raw water. COD Cr 500
Yeast-containing fermentation wastewater having a concentration of 0 mg / L and an SS concentration of 1500 mg / L was continuously passed through to conduct a treatment experiment. The circulating amount of treated water is set to twice the amount of incoming raw water in both experimental devices,
The experimental results are shown in FIG. In the conventional method, when the water flow rate is increased, solids are mixed into the treated water even under a relatively low load condition of 4 kg / m 3 · d of COD Cr , and CO 2
The D Cr removal rate is as low as 80%. In addition, increasing the water flow, C
When the OD Cr volumetric load was 15 kg / m 3 · d, the washout phenomenon of the granules occurred simultaneously with the deterioration of the treated water. On the other hand, in the method of the present invention, the COD Cr volume load 15
Even at kg / m 3 · d, a COD Cr removal rate of 80% or more could be maintained, and almost no solids leaked into the treated water.
【００１５】また、ＣＯＤCr容積負荷１０ｋｇ／ｍ3 ・
ｄにおける反応槽内のｐＨ分布を測定し、測定結果を図
５に示す。なお、図５において、縦軸は水面の高さを１
００としたときの高さ位置を示す。従来法では、酸・メ
タン生成部がはっきり分離していないため、高さ位置に
よりｐＨ変化は認められなった。一方、本発明の方法で
は、酸生成部で固形物が堆積し、酸発酵により可溶化さ
れるため、ｐＨは約５．５まで低下し、メタン生成部で
は処理水の循環で有機酸濃度は希釈されるため、ｐＨは
７付近となった。このように、反応槽内ｐＨ変化が生じ
ており、酸・メタン生成物の分離が行われていることが
分かる。The COD Cr volume load is 10 kg / m 3.
The pH distribution in the reaction tank at d was measured, and the measurement results are shown in FIG. In FIG. 5, the vertical axis indicates the height of the water surface.
The height position when 00 is set is shown. In the conventional method, since the acid / methane generating portion was not clearly separated, no pH change was observed depending on the height position. On the other hand, in the method of the present invention, solids are deposited in the acid generator and solubilized by acid fermentation, so that the pH drops to about 5.5. Due to dilution, the pH was around 7. Thus, it can be seen that the pH in the reaction tank has changed, and the acid / methane product has been separated.
【００１６】[0016]
【発明の効果】本発明によれば、固形物を含む廃水の嫌
気性処理を、１槽式で酸生成、メタン生成それぞれに好
適な条件を維持しながら、グラニュールの活性低下やウ
ォッシュアウトを起こすことなく、効率よく実施するこ
とができる。本発明は、固形物を酸生成部で捕捉し、可
溶化できるため、固形物濃度が高い廃水にも好適に適用
することができる。According to the present invention, the anaerobic treatment of wastewater containing solids can be carried out in a single-tank system while maintaining suitable conditions for acid generation and methane generation while reducing the activity of granules and washing out. It can be implemented efficiently without raising. INDUSTRIAL APPLICABILITY The present invention can capture solids in an acid generator and solubilize the solids, and thus can be suitably applied to wastewater having a high solids concentration.
【図１】本発明の一実施例を示す上向流式嫌気性汚泥床
装置の系統図である。FIG. 1 is a system diagram of an upward anaerobic sludge bed apparatus showing one embodiment of the present invention.
【図２】従来の上向流式嫌気性汚泥床装置の系統図であ
る。FIG. 2 is a system diagram of a conventional upward flow anaerobic sludge bed apparatus.
【図３】グラニュール層の高さ位置と揮発性脂肪酸濃度
の関係を示すグラフである。FIG. 3 is a graph showing a relationship between a height position of a granule layer and a volatile fatty acid concentration.
【図４】実施例１における処理結果を示すグラフであ
る。FIG. 4 is a graph showing a processing result in the first embodiment.
【図５】実施例１における反応槽内の液のｐＨ分布図で
ある。FIG. 5 is a pH distribution diagram of a liquid in a reaction tank in Example 1.
１ 反応槽 ２ 原水ポンプ ３ 酸生成グラニュール層 ４ メタン生成グラニュール層 ５ ガス排出口 ６ 処理水流出口 ７ 処理水槽 ８ 循環ポンプ ９ グラニュール層 １０ 処理水返送口 DESCRIPTION OF SYMBOLS 1 Reaction tank 2 Raw water pump 3 Acid generation granule layer 4 Methane generation granule layer 5 Gas outlet 6 Treated water outlet 7 Treated water tank 8 Circulation pump 9 Granule layer 10 Treated water return port
───────────────────────────────────────────────────── フロントページの続き (72)発明者 遠藤 素子 東京都千代田区内神田１丁目１番14号 日 立プラント建設株式会社内 ──────────────────────────────────────────────────続 き Continuing from the front page (72) Inventor Motoko Endo 1-1-1 Uchikanda, Chiyoda-ku, Tokyo Inside Hitachi Plant Construction Co., Ltd.
Claims (4)
槽に流入させ、該反応槽内の嫌気性微生物群の作用で有
機物を分解する嫌気性生物処理方法において、処理水の
一部を、反応槽内の生物処理部の高さ方向の途中に返送
し、液流速を単一反応槽内で変化させることを特徴とす
る有機性固形物含有廃水の嫌気性生物処理方法。Claims: 1. An anaerobic biological treatment method in which waste water containing organic solids is caused to flow into an anaerobic biological reaction tank and an organic substance is decomposed by the action of anaerobic microorganisms in the reaction tank. An anaerobic biological treatment method for wastewater containing organic solids, wherein the liquid is returned in the height direction of the biological treatment section in the reaction vessel and the liquid flow rate is changed in a single reaction vessel.
処理部の最下部から１／４〜１／３の高さとする請求項
１記載の有機性固形物含有廃水の嫌気性生物処理方法。2. The anaerobic biological treatment of an organic solid-containing wastewater according to claim 1, wherein the position where the treated water is returned to the reaction tank has a height of 1/4 to 1/3 from the lowermost part of the biological treatment section. Method.
槽に流入させ、該反応槽内の嫌気性微生物群の作用で有
機物を分解する嫌気性生物処理装置において、反応槽の
最下部に原水導入配管、反応槽頂部にガス排出口、反応
槽上部に処理水排出配管を有し、さらに処理水を貯留す
る処理水槽を介して、反応槽内の生物処理部の高さ方向
の途中に処理水の一部を返送する処理水返送配管を有す
ることを特徴とする有機性固形物含有廃水の嫌気性生物
処理装置。3. An anaerobic biological treatment apparatus for flowing waste water containing organic solids into an anaerobic biological reaction tank and decomposing organic substances by the action of anaerobic microorganisms in the reaction tank. It has a raw water introduction pipe, a gas outlet at the top of the reaction tank, a treated water discharge pipe at the top of the reaction tank, and a treated water tank that stores treated water, in the middle of the biological treatment section in the reaction tank in the height direction. An anaerobic biological treatment apparatus for treating wastewater containing organic solid matter, comprising a treated water return pipe for returning part of treated water.
の最下部から１／４〜１／３の高さの位置に開口してい
る請求項３記載の有機性固形物含有廃水の嫌気性生物処
理装置。4. The wastewater containing organic solid matter according to claim 3, wherein the treated water return pipe is opened at a height of 1/4 to 1/3 from the lowermost part of the biological treatment section in the reaction tank. Anaerobic biological treatment equipment.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1823598A JPH11197690A (en) | 1998-01-13 | 1998-01-13 | Anaerobic biological treatment method and apparatus for organic solid-containing waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1823598A JPH11197690A (en) | 1998-01-13 | 1998-01-13 | Anaerobic biological treatment method and apparatus for organic solid-containing waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH11197690A true JPH11197690A (en) | 1999-07-27 |
Family
ID=11966022
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1823598A Pending JPH11197690A (en) | 1998-01-13 | 1998-01-13 | Anaerobic biological treatment method and apparatus for organic solid-containing waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH11197690A (en) |
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| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100369924B1 (en) * | 2001-12-28 | 2003-01-30 | 류지순 | Method and system of sewage and waste water treatment |
| KR100710911B1 (en) | 2005-12-27 | 2007-04-27 | 류지순 | A electric-power generation equipment use of waste water |
| JP2011115689A (en) * | 2009-12-01 | 2011-06-16 | Ishigaki Co Ltd | Nitrogen removal apparatus and method |
| JP2012035194A (en) * | 2010-08-06 | 2012-02-23 | Kobelco Eco-Solutions Co Ltd | Anaerobic treatment device and anaerobic treatment method |
| CN102627352A (en) * | 2012-04-17 | 2012-08-08 | 北京师范大学 | Method for catalytically reducing chloronitrobenzene waste water by using straw carbon |
| CN102897909A (en) * | 2011-07-25 | 2013-01-30 | 山东振龙生物化工集团有限公司 | Self-circulation anaerobic reactor |
| JP2013059731A (en) * | 2011-09-14 | 2013-04-04 | Swing Corp | Method and device for anaerobic treatment of pulp mill waste water |
| CN103387287A (en) * | 2013-07-31 | 2013-11-13 | 秦家运 | Carrier biological film upward-filtering anaerobic purifying tank with backwash function |
| CN103408136A (en) * | 2013-08-30 | 2013-11-27 | 中水珠江规划勘测设计有限公司 | Integrated pulse inner cycle anaerobic reaction device |
| CN104445605A (en) * | 2014-11-24 | 2015-03-25 | 南京大学 | Mechanical internal circulation jet-flow anaerobic reactor and wastewater treatment method thereof |
| CN104743660A (en) * | 2013-12-30 | 2015-07-01 | 易百皓源（北京）环保科技有限公司 | New anaerobic sewage treatment pool and sewage treatment method |
| JP2015229150A (en) * | 2014-06-06 | 2015-12-21 | 住友重機械工業株式会社 | Anaerobic treatment apparatus, anaerobic treatment method, and display device of anaerobic treatment apparatus |
-
1998
- 1998-01-13 JP JP1823598A patent/JPH11197690A/en active Pending
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100369924B1 (en) * | 2001-12-28 | 2003-01-30 | 류지순 | Method and system of sewage and waste water treatment |
| KR100710911B1 (en) | 2005-12-27 | 2007-04-27 | 류지순 | A electric-power generation equipment use of waste water |
| JP2011115689A (en) * | 2009-12-01 | 2011-06-16 | Ishigaki Co Ltd | Nitrogen removal apparatus and method |
| JP2012035194A (en) * | 2010-08-06 | 2012-02-23 | Kobelco Eco-Solutions Co Ltd | Anaerobic treatment device and anaerobic treatment method |
| CN102897909A (en) * | 2011-07-25 | 2013-01-30 | 山东振龙生物化工集团有限公司 | Self-circulation anaerobic reactor |
| JP2013059731A (en) * | 2011-09-14 | 2013-04-04 | Swing Corp | Method and device for anaerobic treatment of pulp mill waste water |
| CN102627352A (en) * | 2012-04-17 | 2012-08-08 | 北京师范大学 | Method for catalytically reducing chloronitrobenzene waste water by using straw carbon |
| CN103387287A (en) * | 2013-07-31 | 2013-11-13 | 秦家运 | Carrier biological film upward-filtering anaerobic purifying tank with backwash function |
| CN103408136A (en) * | 2013-08-30 | 2013-11-27 | 中水珠江规划勘测设计有限公司 | Integrated pulse inner cycle anaerobic reaction device |
| CN104743660A (en) * | 2013-12-30 | 2015-07-01 | 易百皓源（北京）环保科技有限公司 | New anaerobic sewage treatment pool and sewage treatment method |
| JP2015229150A (en) * | 2014-06-06 | 2015-12-21 | 住友重機械工業株式会社 | Anaerobic treatment apparatus, anaerobic treatment method, and display device of anaerobic treatment apparatus |
| CN104445605A (en) * | 2014-11-24 | 2015-03-25 | 南京大学 | Mechanical internal circulation jet-flow anaerobic reactor and wastewater treatment method thereof |
| CN104445605B (en) * | 2014-11-24 | 2016-05-18 | 南京大学 | A kind of method of circulating jet anaerobic reactor and processing waste water thereof in machinery |
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