JPH067792A - Organic wastewater treatment method and methane fermentation treatment device - Google Patents
Organic wastewater treatment method and methane fermentation treatment deviceInfo
- Publication number
- JPH067792A JPH067792A JP16750992A JP16750992A JPH067792A JP H067792 A JPH067792 A JP H067792A JP 16750992 A JP16750992 A JP 16750992A JP 16750992 A JP16750992 A JP 16750992A JP H067792 A JPH067792 A JP H067792A
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- Prior art keywords
- treatment
- anaerobic
- raw water
- anaerobic treatment
- organic wastewater
- Prior art date
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Classifications
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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
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Abstract
(57)【要約】 （修正有）
【目的】 嫌気性処理と活性汚泥処理又は硝化・脱窒処
理等の好気性処理との組み合せた生物処理により有機性
排水を処理するにあたり、処理効率の向上及び処理の安
定化を図る。
【構成】 嫌気性処理槽２から発生するメタンガス量を
ガスメータ４及びガス分析計５で測定し、メタンガス量
と嫌気性処理槽２の原水流量（Ｆ1 ）とから、演算制御
装置６で原水のＢＯＤ5 濃度を求め、このＢＯＤ5 濃度
に基き、嫌気性処理槽をバイパスするバイパス原水流量
（Ｆ2 ）を制御する。
(57) [Summary] (Corrected) [Purpose] Improving treatment efficiency when treating organic wastewater by biological treatment combining anaerobic treatment and aerobic treatment such as activated sludge treatment or nitrification / denitrification treatment. And stabilize the processing. [Structure] The amount of methane gas generated from the anaerobic treatment tank 2 is measured by a gas meter 4 and a gas analyzer 5, and from the amount of methane gas and the raw water flow rate (F 1 ) of the anaerobic treatment tank 2, an arithmetic controller 6 is used to control the raw water. The BOD 5 concentration is determined, and based on this BOD 5 concentration, the bypass raw water flow rate (F 2 ) that bypasses the anaerobic treatment tank is controlled.
Description
【０００１】[0001]
【産業上の利用分野】本発明は有機性排水の処理方法及
びメタン発酵処理装置に係り、特に、下水、し尿、産業
排水（食品、化学、紙パルプなど）等の有機性排水を、
嫌気性処理（メタン発酵）と好気性処理とを組み合せた
生物処理により処理するにあたり、排水中の有機物及び
窒素をより効率的にかつ安定して除去する有機性排水の
処理方法及びメタン発酵処理装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a method for treating organic wastewater and a methane fermentation treatment apparatus, and more particularly to treating organic wastewater such as sewage, night soil, industrial wastewater (food, chemistry, paper pulp, etc.)
When treating by biological treatment combining anaerobic treatment (methane fermentation) and aerobic treatment, an organic wastewater treatment method and a methane fermentation treatment device for more efficiently and stably removing organic matter and nitrogen in wastewater Regarding
【０００２】[0002]
【従来の技術】近年、汚泥発生量が少なく、またエネル
ギー消費量の小さい新規排水処理方法として、嫌気性処
理が注目されている。嫌気性処理は、排水中の有機物を
酸生成菌やメタン生成菌などの嫌気性細菌の働きによ
り、最終的にメタンにまで分解するプロセスであり、装
置的には嫌気性固定床、流動床、ＵＡＳＢ（嫌気性汚泥
床）などの諸方法が提案されている。2. Description of the Related Art In recent years, anaerobic treatment has attracted attention as a new wastewater treatment method that produces less sludge and consumes less energy. Anaerobic treatment is a process of finally decomposing organic matter in wastewater into methane by the action of anaerobic bacteria such as acid-producing bacteria and methanogenic bacteria, and in terms of equipment, anaerobic fixed bed, fluidized bed, Various methods such as UASB (anaerobic sludge bed) have been proposed.
【０００３】この嫌気性処理は、省エネルギー的で効率
の高い処理方法ではあるが、嫌気性処理の特徴として、
処理水水質が好気性処理と比較するとやや悪く、処理水
水質は原水濃度によっても異なるが通常ＢＯＤ5 で５０
〜５００ｍｇ／ｌ程度であり、処理水をそのまま公共水
域に放流することはできないという問題点がある。その
ため、通常は嫌気性処理の後段に活性汚泥などの好気性
処理を設置して、放流基準以下まで水質を向上させてい
るのが現状である。This anaerobic treatment is an energy-saving and highly efficient treatment method.
The quality of treated water is slightly worse than that of aerobic treatment, and the quality of treated water varies depending on the concentration of raw water, but usually BOD 5 is 50.
It is about 500 mg / l, and there is a problem that the treated water cannot be discharged as it is to public water bodies. Therefore, it is the current situation that aerobic treatment such as activated sludge is usually installed after the anaerobic treatment to improve the water quality to below the discharge standard.
【０００４】しかし、この組合せ法には次のような問題
点がある。 嫌気性処理により、生物的に容易に分解される基質が
優先的に除去されてしまうため、ＣＯＤcr／ＢＯＤ5 が
原水では１．５〜２であるのに対し、嫌気性処理水では
３〜４程度となる。しかも、同じＢＯＤ5 成分でも、分
解速度の遅い物質が多く残留している。このため、好気
性処理における嫌気性処理水の生物分解性が低い。However, this combination method has the following problems. The anaerobic treatment preferentially removes the biodegradable substrate, so that CODcr / BOD 5 is 1.5 to 2 in raw water, while 3 to 4 in anaerobic treated water. It will be about. Moreover, even with the same BOD 5 component, many substances with a slow decomposition rate remain. Therefore, biodegradability of anaerobic treated water in aerobic treatment is low.
【０００５】嫌気性処理水は生物易分解性の有機物濃
度が低いわりには、ＳＳ性有機物濃度が高い。これは、
嫌気性細菌のうち生物膜やグラニュールを形成しないも
のや、生物膜やグラニュールそのものが、ある程度嫌気
性処理水側に流出するためで、原水濃度が高いほど、そ
の傾向は著しい。嫌気性処理水中の溶解性ＢＯＤ5 が低
すぎると、活性汚泥法などで後処理を行っても、フロッ
クの形成が不十分で、処理水に分散状の汚泥が流出する
だけでなく、後工程の沈殿槽での汚泥の分離が不十分と
なるため、返送汚泥の濃度が十分に上がらず、結果とし
て曝気槽の汚泥濃度が維持できなくなることもある。Although the anaerobic treated water has a low biodegradable organic matter concentration, it has a high SS organic matter concentration. this is,
The anaerobic bacteria that do not form biofilms or granules or the biofilms or granules themselves flow to the anaerobic treated water side to some extent, and the higher the raw water concentration, the more remarkable the tendency. If the solubility BOD 5 in the anaerobic treated water is too low, the flocs are not sufficiently formed even after the post-treatment such as the activated sludge method, and not only the dispersed sludge flows out into the treated water but also the post-process. Since the sludge separation in the settling tank is insufficient, the concentration of the returned sludge may not be sufficiently increased, and as a result, the sludge concentration in the aeration tank may not be maintained.
【０００６】これらの理由から、嫌気性処理の後段に好
気性処理を行なう組合せ法では、十分な好気性処理効果
が得られないことが多い。For these reasons, a combination method in which aerobic treatment is performed after the anaerobic treatment often cannot obtain a sufficient aerobic treatment effect.
【０００７】そこで、活性汚泥などの好気性後処理プロ
セスを良好に機能させる手段として、原水の一部を嫌気
性処理プロセスをバイパスして、直接後段の好気性処理
プロセスに流入させることが提案されている。Therefore, as a means for making the aerobic post-treatment process such as activated sludge function well, it has been proposed that a part of the raw water bypasses the anaerobic treatment process and directly flows into the subsequent aerobic treatment process. ing.
【０００８】[0008]
【発明が解決しようとする課題】しかし、上記の原水の
一部を嫌気性処理プロセスをバイパスして直接後段の活
性汚泥処理プロセスに流入させる方法において（以下、
嫌気性処理プロセスをバイパスして、直接、後処理プロ
セスに流入させる原水を「バイパス原水」と称する場合
がある。）、従来、良好な活性汚泥処理を行うための原
水濃度条件は明らかとされておらず、その制御が難しい
ため、場合によっては好気性処理に問題をきたすことが
ある。However, in the method of directly flowing a part of the raw water into the activated sludge treatment process in the subsequent stage by bypassing the anaerobic treatment process (hereinafter,
Raw water that bypasses the anaerobic treatment process and directly flows into the post-treatment process may be referred to as “bypass raw water”. ), The raw water concentration conditions for performing good activated sludge treatment have not been clarified so far, and its control is difficult, which may cause problems in aerobic treatment in some cases.
【０００９】特に、原水濃度の変動が著しい排水の場
合、原水濃度が上昇した時には、嫌気性処理水とバイパ
ス原水との混合水の濃度も大きく上昇する。このため、
元来、嫌気性処理の後処理のために設計された活性汚泥
処理装置では、その設備容量も小さいため、過負荷とな
り、バルキング等の機能障害を引き起こすこともある。
また、当然、バイパス原水量を増やすほど、汚泥発生量
や通気量の点で嫌気性処理を用いたことによる利点が失
われていくこととなる。In particular, in the case of wastewater whose raw water concentration varies significantly, when the raw water concentration rises, the concentration of the mixed water of the anaerobic treated water and the bypass raw water also greatly rises. For this reason,
An activated sludge treatment device originally designed for post-treatment of anaerobic treatment has a small equipment capacity, and thus may be overloaded and cause functional failures such as bulking.
Further, naturally, as the bypass raw water amount is increased, the advantage of using the anaerobic treatment in terms of sludge generation amount and aeration amount will be lost.
【００１０】一方、主として窒素を除去する必要がある
場合には、嫌気性処理の後段に好気性処理として脱窒
槽、硝酸化槽の２槽を設け、硝酸化槽で生成された硝酸
塩を脱窒槽に戻して、循環法による硝化・脱窒を実施し
ている。この反応は次の、式により、化学量論的に
説明することができる。On the other hand, when it is necessary to mainly remove nitrogen, two tanks, a denitrification tank and a nitrification tank, are provided as an aerobic treatment after the anaerobic treatment, and the nitrate produced in the nitrification tank is denitrified. Then, nitrification and denitrification are carried out by the circulation method. This reaction can be described stoichiometrically by the following equation.
【００１１】 ＮＨ4 +＋２Ｏ2 →ＮＯ3 -＋２Ｈ+ ＋Ｈ2 Ｏ … ６ＮＯ3 -＋５ＣＨ3 ＯＨ→５ＣＯ2 ＋３Ｎ2 ＋７Ｈ2 Ｏ＋６ＯＨ- … この処理法でも、脱窒槽でのＮＯ3 −Ｎの除去率を維持
するためには、水素供与体となる有機物（ＢＯＤ5 ）が
必要である。このため、原水のＢＯＤ5 及びＮ濃度によ
っては、嫌気性処理水の残留ＢＯＤ5 だけでは不十分と
なり、原水を嫌気性処理槽をバイパスさせて脱窒槽に流
入させる必要がある。通常、窒素除去を優先する場合に
は、ＮＯ3 −Ｎからの脱窒反応を重視してそれに必要な
ＢＯＤ5量、即ち、バイパス原水量を十分量とすること
が必要であるが、過度にバイパス原水量を多くすると、
残留ＢＯＤ5 を除去する再曝気槽での負荷が高くなり、
処理が不安定となる。その上、上記ＢＯＤ5 除去の例と
同様、全体としての汚泥発生量も増加することとなり、
嫌気性処理を導入することによる総汚泥発生量の削減効
果が薄れてくるという問題がある。[0011] NH 4 + + 2O 2 → NO 3 - + 2H + + H 2 O ... 6NO 3 - + 5CH 3 OH → 5CO 2 + 3N 2 + 7H 2 O + 6OH - ... In this treatment method, the removal rate of NO 3 -N in the denitrification tank In order to maintain the above, an organic substance (BOD 5 ) which becomes a hydrogen donor is required. For this reason, depending on the BOD 5 and N concentrations of the raw water, the residual BOD 5 of the anaerobic treated water is insufficient, and it is necessary to flow the raw water into the denitrification tank by-passing the anaerobic treatment tank. Usually, when giving priority to nitrogen removal, it is necessary to attach importance to the denitrification reaction from NO 3 —N and to make the amount of BOD 5 required for it, that is, the amount of bypass raw water sufficient, but excessively. When the amount of bypass raw water is increased,
The load on the re-aeration tank for removing residual BOD 5 becomes high,
Processing becomes unstable. Moreover, as with the example of BOD 5 removal above, the amount of sludge generated as a whole increases,
There is a problem that the effect of reducing the total amount of sludge generated by introducing anaerobic treatment is weakened.
【００１２】本発明は上記従来の問題点を解決し、嫌気
性処理と活性汚泥処理又は硝化・脱窒処理等の好気性処
理とを組み合せた生物処理により有機性排水を処理する
にあたり、嫌気性処理プロセスをバイパスして直接好気
性処理プロセスに供給するバイパス原水量の最適量を容
易かつ効率的に求めることにより、処理効率の向上及び
処理の安定化を可能とする有機性排水の処理方法及びメ
タン発酵処理装置を提供することを目的とする。The present invention solves the above-mentioned conventional problems, and treats organic wastewater by biological treatment by combining anaerobic treatment and aerobic treatment such as activated sludge treatment or nitrification / denitrification treatment. A method for treating organic wastewater that enables improvement of treatment efficiency and stabilization of treatment by easily and efficiently determining an optimum amount of bypass raw water that bypasses the treatment process and is directly supplied to the aerobic treatment process, and An object is to provide a methane fermentation treatment device.
【００１３】[0013]
【課題を解決するための手段】請求項１の有機性排水の
処理方法は、有機性排水を嫌気性処理工程に導き、嫌気
処理を行った後、その流出水を、該嫌気性処理工程をバ
イパスする有機性排水と共に好気性処理工程に導き、好
気性処理を行う方法において、前記嫌気性処理工程から
発生するメタンガスの単位通水量当りの発生量を求め、
このメタンガス発生量から前記嫌気性処理工程をバイパ
スして前記好気性処理工程に導かれる有機性排水の流量
を調節することを特徴とする。According to the method for treating organic wastewater of claim 1, the organic wastewater is introduced into an anaerobic treatment step, and after the anaerobic treatment is performed, the effluent is subjected to the anaerobic treatment step. Leading to the aerobic treatment process with the organic wastewater to bypass, in the method of performing aerobic treatment, determine the amount of methane gas generated from the anaerobic treatment step per unit water flow rate,
It is characterized in that the flow rate of the organic waste water introduced into the aerobic treatment step is adjusted by bypassing the anaerobic treatment step from the methane gas generation amount.
【００１４】請求項２のメタン発酵処理装置は、有機性
排水を受入れ、嫌気性処理する嫌気性処理槽と、該嫌気
性処理槽の流出水及び前記有機性排水を受入れ、好気性
処理する好気性処理槽と、前記嫌気性処理槽から発生す
るメタンガス量を測定する手段と、前記嫌気性処理槽に
受入れる有機性排水の流量を測定する手段と、前記メタ
ンガス量及び前記流量の測定結果から有機性排水のＢＯ
Ｄ5 濃度を演算する演算器と、演算されたＢＯＤ5 濃度
の値に基き、前記好気性処理槽に受入れる有機性排水の
流量を制御する制御手段とを備えてなることを特徴とす
る。According to another aspect of the methane fermentation treatment apparatus of the present invention, an anaerobic treatment tank that receives organic wastewater and anaerobically treats it, and a anaerobic treatment tank that receives the effluent of the anaerobic treatment tank and the organic wastewater and aerobically treats it. Gas treatment tank, means for measuring the amount of methane gas generated from the anaerobic treatment tank, means for measuring the flow rate of the organic wastewater received in the anaerobic treatment tank, the methane gas amount and the organic result from the measurement result of the flow rate. BO of natural drainage
It is characterized by comprising a calculator for calculating the D 5 concentration, and a control means for controlling the flow rate of the organic waste water received in the aerobic treatment tank based on the calculated BOD 5 concentration value.
【００１５】[0015]
【作用】本発明者らは、嫌気性処理の後処理としての活
性汚泥処理にて良好な処理を行うための、活性汚泥処理
槽に導入される原水（以下「活性汚泥原水」と称する場
合がある。）の原水濃度条件、即ち、嫌気性処理水とバ
イパス原水との合計の濃度条件について鋭意検討を行っ
たところ、活性汚泥原水の生物易分解性の溶解性ＢＯＤ
5 濃度が１００〜５００ｍｇ／ｌ程度となるように、バ
イパス原水量を調節することが処理効率の向上、処理の
安定化のために重要であることを実験により明らかにし
た。[Advantages] The inventors of the present invention have introduced raw water introduced into an activated sludge treatment tank (hereinafter, referred to as "activated sludge raw water") in order to perform good treatment in activated sludge treatment as a post-treatment of anaerobic treatment. Of the raw water concentration, that is, the total concentration condition of the anaerobic treated water and the bypass raw water, the biodegradable solubility BOD of the activated sludge raw water
It was clarified by experiments that adjusting the amount of bypass raw water so that the concentration of 5 is about 100 to 500 mg / l is important for improving treatment efficiency and stabilizing treatment.
【００１６】また、嫌気性処理の後処理として硝化・脱
窒処理を行なう場合についても、安定な窒素除去を行な
うための、後段の硝化・脱窒プロセスへの流入水（以下
「硝化・脱窒原水」と称する場合がある。）の濃度条件
について鋭意検討を行なったところ、硝化・脱窒原水、
即ち、嫌気性処理水とバイパス原水との合計のＢＯＤ5
と窒素濃度との比を、上記，の反応式に基いて、Ｂ
ＯＤ5 ：Ｎ＝３：１となるように、バイパス原水量を調
節することが重要であることを知見した。Also, when nitrification / denitrification treatment is carried out as a post-treatment of the anaerobic treatment, inflow water to the nitrification / denitrification process of the subsequent stage (hereinafter referred to as “nitrification / denitrification” for stable nitrogen removal). Sometimes referred to as "raw water".), The concentration conditions of the
That is, the total BOD 5 of the anaerobic treated water and the bypass raw water
Based on the above reaction equation, the ratio of
It was found that it is important to adjust the amount of raw bypass water so that OD 5 : N = 3: 1.
【００１７】しかして、バイパス原水量を調節して、活
性汚泥原水又は硝化・脱窒原水のＢＯＤ5 濃度を好適濃
度に安定させるために、原水である有機性排水の濃度を
高価な計測器を必要とすることなく、容易かつ効率的に
検出する手段として、次のような知見に基き、嫌気性処
理工程から発生するメタンガスの単位通水量当りの発生
量を求め、この発生量から好適なバイパス原水量を算出
する手段を見出した。In order to stabilize the BOD 5 concentration of the activated sludge raw water or the nitrification / denitrification raw water to a suitable concentration by adjusting the amount of the bypass raw water, an expensive measuring instrument is used to measure the concentration of the organic waste water as raw water. As a means to detect easily and efficiently without needing it, the amount of methane gas generated from the anaerobic treatment process per unit water flow rate is calculated based on the following knowledge, and a suitable bypass is calculated from this amount. We have found a means to calculate the amount of raw water.
【００１８】即ち、嫌気性処理工程から発生するメタン
ガス量は、処理が安定して行われている限りにおいて
は、原水（有機性排水）の溶解性有機物負荷に正比例す
ることから、ガス発生量及びメタンガス濃度を知ること
により、下記式に従って計算により原水の溶解性有機
物濃度を推定することができる。That is, since the amount of methane gas generated from the anaerobic treatment step is directly proportional to the load of soluble organic matter in the raw water (organic wastewater) as long as the treatment is carried out stably, By knowing the methane gas concentration, the soluble organic matter concentration of the raw water can be estimated by calculation according to the following formula.
【００１９】 原水溶解性ＣＯＤCr(mg/l)≒{(Ｑgas ×Ｆm)／0.35／Ｑin｝×1000 … ただし、Ｑgas ：ガス発生速度（ｍ3 ／ｈｒ） Ｆm ：ガス中のメタンの割合（−） Ｑin ：嫌気性処理工程への通水量（ｍ3 ／ｈｒ） なお、この式中のＦm 、即ちガス中のメタンガスの割合
は、ＣＯ2 濃度検出計又は可燃ガス濃度計などにより連
続的に検出することもできるが、反応槽内のｐＨが安定
していれば、時間的な変動はガス発生量の変化と比較す
ると著しく小さいことから、適宜ガス検知管等により測
定しても差し支えない。Raw water-soluble COD Cr (mg / l) ≈ {(Qgas × Fm) /0.35/Qin} × 1000, where Qgas: gas generation rate (m 3 / hr) Fm: ratio of methane in gas ( -) Qin: Amount of water passed to anaerobic treatment step (m 3 / hr) Note that Fm in this formula, that is, the ratio of methane gas in the gas, is continuously measured by a CO 2 concentration detector or a combustible gas concentration meter. Although it can be detected, if the pH in the reaction tank is stable, the temporal change is significantly smaller than the change in the gas generation amount, and therefore, it may be appropriately measured using a gas detection tube or the like.
【００２０】一方、原水のＣＯＤCrとＢＯＤ5 とにはあ
る一定の関係があるため、定期的に原水のＣＯＤCr及び
ＢＯＤ5 を測定することにより、上記で算出推定した溶
解性ＣＯＤCrから溶解性ＢＯＤ5 を求めることは容易で
ある。Meanwhile, since there is a certain relationship with the the COD Cr and BOD 5 of the raw water, periodically by measuring the COD Cr and BOD 5 of the raw water, dissolved from the soluble COD Cr calculated estimated above It is easy to determine the sex BOD 5 .
【００２１】また、好気性処理と比較して嫌気性処理は
有機物負荷の変動に強いため、嫌気性処理水中の溶解性
ＢＯＤ5 濃度は安定しているので、適宜スポット的に測
定するだけで充分であり、常に監視する必要はない。Further, since the anaerobic treatment is more resistant to the fluctuation of the organic matter load than the aerobic treatment, the concentration of the soluble BOD 5 in the anaerobic treated water is stable, so that it is sufficient to perform spot measurement as appropriate. And does not need to be constantly monitored.
【００２２】従って、変動の大きな原水（有機性排水）
の溶解性ＢＯＤ5 の濃度を、嫌気性処理工程のメタンガ
ス発生量から連続的に算出推定することにより、活性汚
泥原水又は硝化・脱窒原水、即ち、嫌気性処理水及びバ
イパス原水の合計の混合液の溶解性ＢＯＤ5 を知ること
が可能である。Therefore, raw water (organic wastewater) with large fluctuations
By continuously calculating and estimating the concentration of soluble BOD 5 from the amount of methane gas generated in the anaerobic treatment process, the raw water of activated sludge or raw water of nitrification and denitrification, that is, the total mixture of anaerobic treated water and bypass raw water is mixed. It is possible to know the solubility BOD 5 of the liquid.
【００２３】しかして、嫌気性処理と活性汚泥処理との
組み合せによる生物処理においては、活性汚泥原水の溶
解性ＢＯＤ5 濃度が１００〜５００ｍｇ／ｌとなるよう
に、バイパス原水量を制御して、活性汚泥処理に与える
負荷を安定化することにより、嫌気性処理を行なうこと
による利点を最大限に生かしつつ、バルキング、汚泥分
散化などを防ぎ、活性汚泥を効率的、安定的、経済的に
稼働させることができる。However, in the biological treatment by the combination of the anaerobic treatment and the activated sludge treatment, the amount of the bypass raw water is controlled so that the soluble BOD 5 concentration of the activated sludge raw water is 100 to 500 mg / l. By stabilizing the load on activated sludge treatment, while maximizing the advantages of anaerobic treatment, bulking and sludge dispersion are prevented, and activated sludge is operated efficiently, stably, and economically. Can be made.
【００２４】また、嫌気性処理と硝化・脱窒処理との組
み合せによる生物処理においては、硝化・脱窒原水の溶
解性ＢＯＤ5 濃度がＮ濃度の３倍強となるように、それ
ぞれバイパス原水量を制御することにより、硝化・脱窒
処理への生物易分解性の有機物負荷を安定化することに
より、脱窒反応に必要な最適な水素供与体量を維持する
ことができ、これにより、嫌気性処理を行うことによる
利点を最大限に生かし、より安定して、経済的に窒素除
去を行なうことが可能となる。Further, in the biological treatment by the combination of the anaerobic treatment and the nitrification / denitrification treatment, the amount of bypass raw water is adjusted so that the solubility BOD 5 concentration of the nitrification / denitrification raw water becomes slightly more than 3 times the N concentration. By controlling the nitrogen content, it is possible to maintain the optimum amount of hydrogen donors necessary for the denitrification reaction by stabilizing the load of easily biodegradable organic substances on the nitrification / denitrification process. It is possible to make the most of the advantages of the chemical treatment and to perform nitrogen removal more stably and economically.
【００２５】因みに、現状において、バイパス原水量を
正確に制御するためには、原水（有機性排水）濃度及び
嫌気性処理水の溶解性ＢＯＤ5 濃度をオンラインで測定
することが必要であるが、従来、その様な目的の濃度測
定装置はなく、可能な手段として最良のものでも、サン
プルを濾過してそのＴＯＣ（ＣＯＤ）等を半連続的に測
定する程度である。しかし、この方法ではＴＯＣ自動測
定装置などの計測器に多大な費用がかかる。本発明で
は、こうした濃度測定のための高価な計測器を必要とせ
ずに、バイパス量を制御して後処理プロセスへの原水濃
度を安定に維持することができる。Incidentally, at present, it is necessary to measure the raw water (organic wastewater) concentration and the soluble BOD 5 concentration of the anaerobic treated water online in order to accurately control the bypass raw water amount. Conventionally, there is no such concentration measuring device for the purpose, and even the best possible means is to measure the TOC (COD) and the like semi-continuously by filtering the sample. However, this method requires a great deal of cost for a measuring instrument such as a TOC automatic measuring device. In the present invention, it is possible to control the amount of bypass and maintain a stable raw water concentration for the post-treatment process without requiring an expensive measuring instrument for such concentration measurement.
【００２６】[0026]
【実施例】以下、図面を参照して本発明の実施例につい
て詳細に説明する。Embodiments of the present invention will now be described in detail with reference to the drawings.
【００２７】図１は、本発明のメタン発酵処理装置の一
実施例を示す系統図である。FIG. 1 is a system diagram showing an embodiment of the methane fermentation treatment apparatus of the present invention.
【００２８】図１において、１は原水槽、２はＵＡＳ
Ｂ，固定床又は流動床等の嫌気性処理槽、３は活性汚泥
又は硝化・脱窒等の好気性処理槽、４はガスメータ、５
はガス分析計、６は演算制御装置である。１１は、原水
槽１内の原水を嫌気性処理槽２に送給する配管であり、
ポンプＰ1 と流量計Ｆ1 とを備える。１２は嫌気性処理
水を好気性処理槽３に送給する配管、１３は処理水を系
外へ排出する配管である。１４は原水槽１の原水を直接
好気性処理槽３に送給する配管であり、ポンプＰ2 と流
量計Ｆ2 とを備える。１５は嫌気性処理槽２で発生した
ガスをガスメータ４に送給する配管である。In FIG. 1, 1 is a raw water tank and 2 is a UAS.
B, anaerobic treatment tank such as fixed bed or fluidized bed, 3 aerobic treatment tank for activated sludge or nitrification / denitrification, 4 gas meter, 5
Is a gas analyzer, and 6 is an arithmetic and control unit. Reference numeral 11 is a pipe for feeding the raw water in the raw water tank 1 to the anaerobic treatment tank 2,
A pump P 1 and a flow meter F 1 are provided. Reference numeral 12 is a pipe for feeding the anaerobic treated water to the aerobic treatment tank 3, and 13 is a pipe for discharging the treated water to the outside of the system. Reference numeral 14 is a pipe for directly feeding the raw water from the raw water tank 1 to the aerobic treatment tank 3, which is provided with a pump P 2 and a flow meter F 2 . Reference numeral 15 is a pipe for feeding the gas generated in the anaerobic treatment tank 2 to the gas meter 4.
【００２９】即ち、嫌気性処理槽２には、発生するガス
量を測定するガスメータ４及び発生するガス中のメタン
濃度を分析するガス分析計５が接続されており、また、
これらの測定結果が入力される演算装置６が設けられて
いる。ポンプＰ1 による流量計Ｆ1 の測定結果もこの演
算装置６に入力され、一方、ポンプＰ2 による流量計Ｆ
2 の流量は、この演算装置６の結果に基き増減されるよ
うに構成されている。That is, the anaerobic treatment tank 2 is connected with a gas meter 4 for measuring the amount of generated gas and a gas analyzer 5 for analyzing the concentration of methane in the generated gas, and
An arithmetic unit 6 to which these measurement results are input is provided. Measurements of the flow meter F 1 by the pump P 1 is also input to the computing device, while the flowmeter F by the pump P 2
The flow rate of 2 is configured to be increased or decreased based on the result of the arithmetic unit 6.
【００３０】本実施例のメタン発酵処理装置において
は、原水槽１内の原水を配管１１より嫌気性処理槽２に
送給して嫌気性処理し、嫌気性処理水は配管１２を経て
好気性処理水に送給する。一方、原水槽１の原水の一部
は配管１４より直接好気性処理槽３に送給される。好気
性処理槽３の処理水は配管１３より系外へ排出される。In the methane fermentation treatment apparatus of this embodiment, the raw water in the raw water tank 1 is fed from the pipe 11 to the anaerobic treatment tank 2 for anaerobic treatment, and the anaerobic treated water is aerobic through the pipe 12. Deliver to treated water. On the other hand, a part of the raw water in the raw water tank 1 is directly fed to the aerobic treatment tank 3 through the pipe 14. The treated water in the aerobic treatment tank 3 is discharged from the system through the pipe 13.
【００３１】嫌気性処理槽２の発生ガスは、配管１５よ
りガスメータ４に送給され、ガスメータ４にて連続的に
測定され、更に、ガス中のメタンガス濃度がガス分析計
５により連続的に測定され、測定結果は演算制御装置６
に入力される。また、配管１１より嫌気性処理槽２に導
入される原水の流量は、流量計Ｆ1 により測定され、こ
の測定値も演算制御装置６に入力される。The gas generated in the anaerobic treatment tank 2 is fed to the gas meter 4 through the pipe 15 and continuously measured by the gas meter 4, and the methane gas concentration in the gas is continuously measured by the gas analyzer 5. The measurement result is calculated and the arithmetic and control unit 6
Entered in. Further, the flow rate of the raw water introduced into the anaerobic treatment tank 2 through the pipe 11 is measured by the flow meter F 1 , and this measured value is also input to the arithmetic and control unit 6.
【００３２】この演算制御装置６に入力された発生ガス
量、メタンガス濃度及び嫌気性処理槽２への原水流量よ
り、前記式から原水中の溶解性ＣＯＤCr濃度が求めら
れる。この溶解性ＣＯＤCr濃度より、溶解性ＢＯＤ5 濃
度を推定し、嫌気性処理水とバイパス原水量との混合液
である好気性処理槽３の原水溶解性ＢＯＤ5 濃度が所定
の濃度となるように、流量計Ｆ2 のバイパス原水量を定
め、演算制御装置６よりポンプＰ2 の制御信号を出力す
る。From the above equation, the soluble COD Cr concentration in the raw water can be obtained from the amount of generated gas, the methane gas concentration, and the raw water flow rate to the anaerobic treatment tank 2, which are input to the arithmetic and control unit 6. The soluble BOD 5 concentration is estimated from this soluble COD Cr concentration so that the raw water-soluble BOD 5 concentration in the aerobic treatment tank 3, which is a mixed solution of the anaerobic treated water and the bypass raw water amount, becomes a predetermined concentration. Then, the bypass raw water amount of the flow meter F 2 is determined, and the control signal of the pump P 2 is output from the arithmetic and control unit 6.
【００３３】なお、ガスメータ４としては、容積式（湿
式、乾式）、サーマルフロー式等、様々な形式のものを
用いることができる。このガスメータ４の前段にＣＯ2
除去カラムを設置しても良く、この場合には、メタン濃
度の測定は不要となる。As the gas meter 4, various types such as a volume type (wet type, dry type) and a thermal flow type can be used. CO 2 is placed in front of this gas meter 4.
A removal column may be installed, and in this case, measurement of methane concentration becomes unnecessary.
【００３４】また、ガス分析計５は、連続的にメタン濃
度を測定するものの他、１日に１回程度実施されるガス
検知管等を利用したメタン濃度測定手段であっても良
い。Further, the gas analyzer 5 may be one for continuously measuring the methane concentration, or may be a methane concentration measuring means using a gas detector tube or the like which is carried out about once a day.
【００３５】なお、本発明において、好気性処理として
は、活性汚泥、硝化・脱窒に限らず、好気性濾床、深層
曝気等の他の好気性処理にも適用することができ、いず
れの場合においてもバイパス原水量を最適量に制御し
て、良好な嫌気処理及び好気処理を行うことができるこ
とは言うまでもない。In the present invention, the aerobic treatment is not limited to activated sludge and nitrification / denitrification, but can be applied to other aerobic treatments such as aerobic filter bed and deep aeration. Even in such a case, it goes without saying that the bypass raw water amount can be controlled to an optimum amount to perform good anaerobic treatment and aerobic treatment.
【００３６】[0036]
【発明の効果】以上詳述した通り、本発明の有機性排水
の処理方法及びメタン発酵処理装置によれば、有機性排
水を嫌気性処理と好気性処理との組み合せによる生物処
理で処理するにあたり、嫌気性処理工程をバイパスして
直接好気性処理に流入させる原水量を、高価な濃度計測
器を必要とすることなく、容易かつ効率的に最適量に調
節することができる。従って、嫌気性処理を採用するこ
とによる汚泥発生量の低減、消費エネルギー量の低減等
の効果を十分に発揮させつつ、後段の好気性処理により
高い処理効率にて安定な好気性処理を行なって、高水質
の処理水を容易かつ効率的に得ることが可能とされる。As described in detail above, according to the method for treating organic wastewater and the methane fermentation treatment apparatus of the present invention, when treating organic wastewater by biological treatment by a combination of anaerobic treatment and aerobic treatment. The amount of raw water that bypasses the anaerobic treatment process and flows directly into the aerobic treatment can be easily and efficiently adjusted to the optimum amount without requiring an expensive concentration measuring device. Therefore, while making full use of the effects of reducing the amount of sludge generated and energy consumption by adopting the anaerobic treatment, a stable aerobic treatment with high treatment efficiency can be performed by the latter aerobic treatment. It is possible to easily and efficiently obtain treated water of high quality.
【図１】本発明のメタン発酵処理装置の一実施例を示す
系統図である。FIG. 1 is a system diagram showing an embodiment of a methane fermentation treatment apparatus of the present invention.
１ 原水槽 ２ 嫌気性処理槽 ３ 好気性処理槽 ４ ガスメータ ５ ガス分析計 ６ 演算制御装置 1 Raw water tank 2 Anaerobic treatment tank 3 Aerobic treatment tank 4 Gas meter 5 Gas analyzer 6 Arithmetic control device
Claims (2)
気処理を行った後、その流出水を、該嫌気性処理工程を
バイパスする有機性排水と共に好気性処理工程に導き、
好気性処理を行う方法において、 前記嫌気性処理工程から発生するメタンガスの単位通水
量当りの発生量を求め、 このメタンガス発生量から前記嫌気性処理工程をバイパ
スして前記好気性処理工程に導かれる有機性排水の流量
を調節することを特徴とする有機性排水の処理方法。1. The organic wastewater is introduced into an anaerobic treatment step, and after the anaerobic treatment, the outflow water is introduced into an aerobic treatment step together with the organic wastewater bypassing the anaerobic treatment step,
In the method of performing aerobic treatment, the generation amount of methane gas generated from the anaerobic treatment process per unit amount of water flow is obtained, and the anaerobic treatment process is bypassed from the methane gas generation amount and guided to the aerobic treatment process. A method for treating organic wastewater, which comprises controlling the flow rate of the organic wastewater.
気性処理槽と、 該嫌気性処理槽の流出水及び前記有機性排水を受入れ、
好気性処理する好気性処理槽と、 前記嫌気性処理槽から発生するメタンガス量を測定する
手段と、 前記嫌気性処理槽に受入れる有機性排水の流量を測定す
る手段と、 前記メタンガス量及び前記流量の測定結果から有機性排
水のＢＯＤ5 濃度を演算する演算器と、 演算されたＢＯＤ5 濃度の値に基き、前記好気性処理槽
に受入れる有機性排水の流量を制御する制御手段とを備
えてなることを特徴とするメタン発酵処理装置。2. An anaerobic treatment tank which receives organic wastewater and anaerobically treats it, and a effluent of the anaerobic treatment tank and the organic wastewater,
Aerobic treatment tank for aerobic treatment, means for measuring the amount of methane gas generated from the anaerobic treatment tank, means for measuring the flow rate of organic wastewater received in the anaerobic treatment tank, the methane gas amount and the flow rate and measurements calculator for calculating the BOD 5 concentration of the organic waste water from, based on the value of the computed BOD 5 concentrations, and control means for controlling the flow rate of organic wastewater to accept the aerobic treatment tank A methane fermentation treatment device characterized by:
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16750992A JP3203774B2 (en) | 1992-06-25 | 1992-06-25 | Organic wastewater treatment method and methane fermentation treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP16750992A JP3203774B2 (en) | 1992-06-25 | 1992-06-25 | Organic wastewater treatment method and methane fermentation treatment device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH067792A true JPH067792A (en) | 1994-01-18 |
| JP3203774B2 JP3203774B2 (en) | 2001-08-27 |
Family
ID=15851004
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP16750992A Expired - Lifetime JP3203774B2 (en) | 1992-06-25 | 1992-06-25 | Organic wastewater treatment method and methane fermentation treatment device |
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| Country | Link |
|---|---|
| JP (1) | JP3203774B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH09290293A (en) * | 1996-04-25 | 1997-11-11 | Daikin Ind Ltd | Fluid purification device |
| JP2000015231A (en) * | 1998-07-06 | 2000-01-18 | Kubota Corp | Methane fermentation method for organic waste |
| JP2001252686A (en) * | 2000-03-10 | 2001-09-18 | Kurita Water Ind Ltd | Anaerobic treatment of organic wastewater |
| JP2003071497A (en) * | 2001-09-03 | 2003-03-11 | Ishikawajima Harima Heavy Ind Co Ltd | Organic waste treatment method and treatment device |
| JP2007237055A (en) * | 2006-03-07 | 2007-09-20 | Toshiba Corp | Method and apparatus for treating organic wastewater |
| JP2012192320A (en) * | 2011-03-15 | 2012-10-11 | Toshiba Corp | Organic wastewater treatment apparatus |
| JP2012206043A (en) * | 2011-03-30 | 2012-10-25 | Kurita Water Ind Ltd | Treatment apparatus of organic wastewater |
-
1992
- 1992-06-25 JP JP16750992A patent/JP3203774B2/en not_active Expired - Lifetime
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH09290293A (en) * | 1996-04-25 | 1997-11-11 | Daikin Ind Ltd | Fluid purification device |
| JP2000015231A (en) * | 1998-07-06 | 2000-01-18 | Kubota Corp | Methane fermentation method for organic waste |
| JP2001252686A (en) * | 2000-03-10 | 2001-09-18 | Kurita Water Ind Ltd | Anaerobic treatment of organic wastewater |
| JP2003071497A (en) * | 2001-09-03 | 2003-03-11 | Ishikawajima Harima Heavy Ind Co Ltd | Organic waste treatment method and treatment device |
| JP2007237055A (en) * | 2006-03-07 | 2007-09-20 | Toshiba Corp | Method and apparatus for treating organic wastewater |
| JP2012192320A (en) * | 2011-03-15 | 2012-10-11 | Toshiba Corp | Organic wastewater treatment apparatus |
| JP2012206043A (en) * | 2011-03-30 | 2012-10-25 | Kurita Water Ind Ltd | Treatment apparatus of organic wastewater |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3203774B2 (en) | 2001-08-27 |
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