JP2011110507A - Anaerobic treatment method and apparatus - Google Patents
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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
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- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
本発明は、食品工場、化学工場などの各種工場より排出される有機性廃水を対象とし、酸発酵工程とメタン発酵工程からなる二相式嫌気性処理方法及び装置に関し、さらに詳しくは酸発酵工程での酸発酵不良を簡便かつ迅速に検知することで安定した処理のできる二相式嫌気性処理方法及び装置に関する。 The present invention is directed to organic wastewater discharged from various factories such as food factories and chemical factories, and relates to a two-phase anaerobic treatment method and apparatus comprising an acid fermentation process and a methane fermentation process, and more specifically, an acid fermentation process. The present invention relates to a two-phase anaerobic treatment method and apparatus capable of performing stable treatment by simply and quickly detecting poor acid fermentation.
有機性廃水は、嫌気性処理によって分解処理される。嫌気性処理は、数多くの細菌類やいくつもの中間代謝過程が関与するような複雑なプロセスによって成り立っている。嫌気性処理は、大きく酸発酵工程とメタン発酵工程に分けられる。酸発酵工程では、先ず、炭水化物やたんぱく質、脂質などの複雑な有機化合物が加水分解によって、糖、アミノ酸、ペプチド等の低分子の有機物に分解され、分解された有機物は、酸発酵によって揮発性有機酸に分解される。次に、長鎖の揮発性有機酸（ＶＦＡ）が、酢酸生成細菌によって酢酸と水素に変換される。続くメタン発酵工程では、メタン生成細菌によって酢酸、蟻酸、水素、メタノール等からメタンに変換される。このように、メタン生成細菌は、基質として処理できる物質が限られているため、廃水中の有機物を有機酸等に転換する酸発酵工程は重要となる。 Organic wastewater is decomposed by anaerobic treatment. Anaerobic treatment consists of a complex process involving many bacteria and several intermediate metabolic processes. Anaerobic treatment is roughly divided into an acid fermentation process and a methane fermentation process. In the acid fermentation process, first, complex organic compounds such as carbohydrates, proteins, and lipids are decomposed into low-molecular organic substances such as sugars, amino acids, and peptides by hydrolysis, and the decomposed organic substances are volatile organic by acid fermentation. Decomposed into acid. The long chain volatile organic acid (VFA) is then converted to acetic acid and hydrogen by acetic acid producing bacteria. In the subsequent methane fermentation process, acetic acid, formic acid, hydrogen, methanol, etc. are converted into methane by methanogenic bacteria. Thus, since methanogenic bacteria have limited substances that can be treated as substrates, an acid fermentation process that converts organic substances in wastewater into organic acids or the like is important.
嫌気性処理は、大きく一相式嫌気性処理と二相式嫌気性処理に分けられる。一相式嫌気性処理は、主に酸発酵を行う酸発酵工程と主にメタン発酵を行うメタン発酵工程を同一槽内で行う処理方法であり、二相式嫌気性処理は、酸発酵工程とメタン発酵工程を２槽にわけて行う処理方法である。二相式嫌気性処理の特徴としては、（１）一相式より二相式嫌気性処理の方がＣＯＤ除去量が多く、プロセスの安定性も勝ること、（２）酸発酵の最適ｐＨの観点から、酸発酵槽内ｐＨは５．０〜６．５であるのに対し、メタン発酵の最適ｐＨは６．５〜８．５に設定されることから、ｐＨ調整が容易であることにある。
高分子の有機物を含む原水を、一相式嫌気性処理方式で処理する場合、高分子の有機物の酸発酵工程が律速条件となるため発酵処理装置での滞留時間が長くなるので、設備が過大となり、効率の良い処理が行われない。高分子の有機物を含む原水を対象とする場合には、メタン発酵工程の前段に酸発酵工程を設けた二相式嫌気性処理方式とし、酸発酵工程で高分子の有機物を有機酸あるいは比較的低分子の有機物へ転換させるのがよい。これによって、メタン発酵工程の滞留時間が短くなり、一相式嫌気性処理方式と比べて効率の良い処理が実現できる。
Anaerobic treatment is roughly divided into one-phase anaerobic treatment and two-phase anaerobic treatment. The one-phase anaerobic treatment is a treatment method in which the acid fermentation process that mainly performs acid fermentation and the methane fermentation process that mainly performs methane fermentation are performed in the same tank. It is the processing method which divides a methane fermentation process into two tanks. The characteristics of the two-phase anaerobic treatment are as follows: (1) The two-phase anaerobic treatment has a higher COD removal amount and the process stability is better than the one-phase type, and (2) the optimum pH of acid fermentation. From the viewpoint, the pH in the acid fermenter is 5.0 to 6.5, whereas the optimum pH for methane fermentation is set to 6.5 to 8.5, so that pH adjustment is easy. is there.
When raw water containing high-molecular organic substances is treated with a one-phase anaerobic treatment method, the acid fermentation process of high-molecular organic substances becomes the rate-determining condition, so the residence time in the fermentation treatment equipment becomes longer, so the facilities are excessive. Thus, efficient processing is not performed. When raw water containing high-molecular organic substances is targeted, a two-phase anaerobic treatment method is provided in which an acid fermentation process is provided before the methane fermentation process. It is better to convert it to a low molecular organic substance. Thereby, the residence time of a methane fermentation process becomes short, and an efficient process is realizable compared with the one phase type anaerobic processing system.
比較的高分子の有機物としては、タンパク質や脂質やでんぷん等が例としてあげられる。また、マルチトールやキシリトール等の糖アルコール等の難発酵成分も、高分子の有機物と同様に酸発酵工程が律速となる場合が多い。これらを合わせて難発酵成分と記す。
処理対象となる有機性廃水に含まれる難発酵成分の割合が高い場合、酸発酵工程において、難発酵成分の低分子化や有機酸への転換が十分に進行しない状態（この状態を以下、酸発酵不良とも記す）になる恐れがある。この状態の酸発酵槽流出水をメタン発酵処理する場合、メタン発酵工程の処理性能が低下し、メタン発酵槽流出水中には、残留ＶＦＡ、未分解の有機物が含まれるとみられる。また、難発酵成分の低分子化や有機酸への転換が、十分に進行していないメタン発酵流出水を循環水として利用する場合、循環水由来の負荷がメタン発酵工程にかかり、さらにメタン発酵工程の処理性能が低下することになる。
さらに、酸発酵不良が悪化すると、メタン発酵工程のｐＨは、メタン発酵に適した６．５〜８．５の範囲を下回ることになる。この状態では、メタン発酵は停止し、さらにメタン発酵菌が死滅する状態（この状態を以下、酸敗とも記す）になる。
Examples of relatively high molecular organic substances include proteins, lipids, and starches. In addition, difficult-fermentable components such as sugar alcohols such as maltitol and xylitol often have a rate-determining rate in the acid fermentation process, as in the case of high molecular organic substances. These are collectively referred to as difficult-to-ferment components.
When the proportion of difficult-to-ferment components contained in the organic wastewater to be treated is high, the acid fermentation process does not proceed sufficiently to reduce the molecular weight of the difficult-to-ferment components or to convert to organic acids (this state is referred to as acid (It is also described as poor fermentation). When the acid fermenter effluent in this state is subjected to methane fermentation treatment, the processing performance of the methane fermentation process is lowered, and the methane fermenter effluent is considered to contain residual VFA and undecomposed organic matter. In addition, when methane fermentation effluent that has not been sufficiently progressed to reduce the molecular weight of difficult-to-ferment components or convert to organic acids is used as circulating water, the load from the circulating water is applied to the methane fermentation process, and methane fermentation The processing performance of a process will fall.
Furthermore, if the acid fermentation defect deteriorates, the pH of the methane fermentation process falls below the range of 6.5 to 8.5 suitable for methane fermentation. In this state, the methane fermentation is stopped, and further, the methane fermentation bacteria are killed (this state is hereinafter also referred to as an acid loss).
菌体が倍増する倍化時間は、メタン発酵菌で８３時間といわれ、酸発酵菌の３３時間、活性汚泥の３．５時間と比べて非常に長い。いったん酸敗により、メタン発酵菌が死滅すると、処理性能が回復するまでに長期間を要する。
嫌気性処理装置を安定的に運転するために、特開平１０−２３５３９１号公報では、二相式嫌気性排水処理装置において、酸生成槽におけるＣＯＤ負荷あたりのアルカリ添加量が許容範囲を超えたことを検知することで、処理水に有機酸が残存した処理悪化の状態と判定して、負荷低減の制御を行う方法が示されている。
また、特開平７−１７１５９２号公報では、原水ＣＯＤＣｒとメタンガス発生量から、ガス化率を算出し、ガス化率から処理能力を判定して流入原水量を調節する方法が示されている。
The doubling time for doubling the cells is said to be 83 hours for methane-fermenting bacteria, which is much longer than 33 hours for acid-fermenting bacteria and 3.5 hours for activated sludge. Once the methane-fermenting bacteria are killed due to rancidity, it takes a long time for the treatment performance to recover.
In order to stably operate the anaerobic treatment apparatus, in Japanese Patent Laid-Open No. 10-235391, in the two-phase anaerobic wastewater treatment apparatus, the amount of alkali added per COD load in the acid generation tank exceeds the allowable range. By detecting this, it is determined that the organic acid remains in the treated water and is in a deteriorated state of treatment, and a method for controlling the load reduction is shown.
Japanese Patent Application Laid-Open No. 7-171592 discloses a method of adjusting the inflow raw water amount by calculating the gasification rate from the raw water COD Cr and the amount of methane gas generated and determining the treatment capacity from the gasification rate.
しかしながら、二相式嫌気処理方式の安定運転に関しては以下に示すような問題点がある。
（１） 難発酵成分を含んだ有機性廃水では、難発酵成分の割合が高まると、難発酵成分を低分子化及び有機酸に転換するのに要する滞留時間が不足する状態になりやすく、酸発酵不良を生じる恐れや、酸発酵槽における酸発酵不良に伴いメタン発酵槽内が酸敗状態となりメタン発酵処理性能が低下する恐れが高い。
（２） 従来法の酸発酵工程でのアルカリ添加量が許容範囲を超えた場合に負荷制御を行う方法では、有機酸が残留しｐＨが低下した状態のメタン発酵処理水を、酸発酵工程に循環している状態であり、上記の負荷制御を行ってもメタン発酵処理性能が回復しない恐れが高い。
（３） 原水ＣＯＤＣｒとメタンガス発生量から算出したガス化率をもとに、流入原水量を調節する方法では、ガス化率の低下を検知した状態は既にメタン発酵処理性能が低下している状態であり、上記の負荷制御を行ってもメタン発酵処理性能が回復しない恐れが高い。
(1) In organic wastewater containing difficult-to-ferment components, when the proportion of difficult-to-ferment components increases, the residence time required for converting the difficult-to-ferment components into low molecular weight and organic acids tends to be insufficient. There is a high risk of causing a fermentation failure or a deterioration of the methane fermentation treatment performance due to the acid fermentation failure in the acid fermentation tank and the inside of the methane fermentation tank becoming in an acidified state.
(2) In the method of performing load control when the amount of alkali added in the conventional acid fermentation process exceeds the allowable range, the methane fermentation treated water in which the organic acid remains and the pH is lowered is used as the acid fermentation process. It is in a circulating state, and there is a high possibility that the performance of methane fermentation treatment will not recover even if the load control is performed.
(3) In the method of adjusting the inflow raw water amount based on the gasification rate calculated from the raw water COD Cr and the amount of methane gas generated, the state in which the gasification rate is detected has already deteriorated in the methane fermentation treatment performance. There is a high possibility that the methane fermentation treatment performance will not be restored even if the load control is performed.
本発明は、上記従来技術の問題点を解決するために、難発酵成分を含んだ有機性廃水を処理する場合に際して、酸発酵工程における酸発酵不良の迅速検知を行い、メタン発酵処理性能の低下を未然に防ぐことができる嫌気性処理方法及び装置を提供することを課題とする。 In order to solve the above-mentioned problems of the prior art, the present invention performs rapid detection of acid fermentation failure in an acid fermentation process when processing organic wastewater containing difficult-to-ferment components, and reduces methane fermentation treatment performance. It is an object of the present invention to provide an anaerobic treatment method and apparatus capable of preventing the above.
上記課題を解決するために、本発明では、有機性廃水を、アルカリ剤を用いてｐＨ値を制御しながら酸発酵工程とメタン発酵工程を順次通して処理する二相式の嫌気性処理方法において、前記酸発酵工程でｐＨ値を制御するために添加するアルカリ剤の注入量が、該酸発酵工程へ流入する流入水の有機物負荷量より求めたアルカリ剤注入率の設定値以下になったときに、該酸発酵工程へ流入する前記廃水の流入量を減少又は停止することを特徴とする有機性廃水の嫌気性処理方法としたものである。
前記嫌気性処理方法において、ｐＨ値の制御は、酸発酵工程のｐＨが５．０〜６．５、メタン発酵工程のｐＨが６．５〜８．５になるように行うのがよく、前記有機物負荷量は、流入水中の有機物濃度と流入水の流入量から算出することができ、また、前記メタン発酵工程では、流出水の一部を前記酸発酵工程及び／又は該メタン発酵工程に循環することができ、その際、前記メタン発酵工程からの流出水を酸発酵工程及び／又はメタン発酵工程に循環する循環水は、前記酸発酵工程で、ｐＨ値を制御するために添加するアルカリ剤の注入量が、流入水の有機物負荷量より求めたアルカリ剤注入率の設定値以下になったときに、減少又は停止するのがよい。
In order to solve the above problems, in the present invention, in a two-phase anaerobic treatment method in which organic wastewater is treated through an acid fermentation step and a methane fermentation step sequentially while controlling the pH value using an alkaline agent. When the injection amount of the alkaline agent added to control the pH value in the acid fermentation step is equal to or less than the set value of the alkaline agent injection rate obtained from the organic load amount of the influent water flowing into the acid fermentation step Furthermore, an anaerobic treatment method for organic wastewater is characterized in that the amount of wastewater flowing into the acid fermentation process is reduced or stopped.
In the anaerobic treatment method, the pH value is preferably controlled so that the pH in the acid fermentation process is 5.0 to 6.5 and the pH in the methane fermentation process is 6.5 to 8.5. The amount of organic matter load can be calculated from the concentration of organic matter in the influent water and the inflow amount of the influent water. In the methane fermentation process, a part of the effluent is circulated to the acid fermentation process and / or the methane fermentation process. In this case, the circulating water that circulates the effluent from the methane fermentation process to the acid fermentation process and / or the methane fermentation process is added to control the pH value in the acid fermentation process. It is preferable to reduce or stop the injection amount when the amount becomes less than the set value of the alkali agent injection rate obtained from the organic matter load amount of the influent water.
また、本発明では、有機性廃水を酸発酵する酸発酵槽と、該酸発酵槽からの流出水をメタン発酵するメタン発酵槽と、酸発酵槽中のｐＨ値を検出する手段と、検出したｐＨ値に基づいて注入するアルカリ剤の注入量を検出する手段とを備えた二相式の嫌気性処理装置において、前記有機性廃水が酸発酵槽へ流入する流入量を検出して制御する流量制御手段と、該廃水の有機物濃度検出手段とを備え、前記アルカリ剤の注入量と、前記廃水の酸発酵槽へ流入する流入量と有機物濃度から算出された有機物負荷量から求めたアルカリ剤注入率の設定値とに基づいて、前記酸発酵槽へ流入する前記廃水の流入量を制御する機構を備えたことを特徴とする有機性廃水の嫌気性処理装置としたものである。
前記嫌気性処理装置において、前記メタン発酵槽は、流出水の一部を前記酸発酵槽及び／又は該メタン発酵槽に循環する経路を有することができ、該経路には、前記流出水の循環量を制御する流量制御手段を有し、前記アルカリ剤の注入量と、前記有機物負荷量から求めたアルカリ剤注入率の設定値に基づいて、循環水の循環量を制御する機構を備えることができる。
Further, in the present invention, an acid fermenter for acid fermentation of organic waste water, a methane fermenter for methane fermentation of effluent from the acid fermenter, and means for detecting a pH value in the acid fermenter are detected. In a two-phase anaerobic treatment apparatus comprising a means for detecting the injection amount of an alkaline agent to be injected based on the pH value, a flow rate for detecting and controlling the inflow amount of the organic wastewater flowing into the acid fermentation tank An alkaline agent injection determined from an injection amount of the alkaline agent, an inflow amount flowing into the acid fermenter of the waste water and an organic substance load amount calculated from the organic substance concentration; An anaerobic treatment apparatus for organic wastewater comprising a mechanism for controlling the amount of inflow of the wastewater flowing into the acid fermentation tank based on the set value of the rate.
In the anaerobic treatment apparatus, the methane fermentation tank may have a path for circulating a part of the effluent water to the acid fermentation tank and / or the methane fermentation tank, and the path includes circulation of the effluent water. It has a flow rate control means for controlling the amount, and has a mechanism for controlling the amount of circulating water based on the injection amount of the alkali agent and the set value of the alkali agent injection rate obtained from the organic material load amount. it can.
本発明の方法により、酸発酵不良の迅速な検知によって、流入有機物負荷量を減少及び／又は滞留時間を増加させることで、酸発酵不良が発生してもメタン発酵処理性能の低下を回避し、さらにはメタン発酵菌を死滅させることがなく、難発酵物質流入後の溶解性ＣＯＤＣｒ除去率を従来法より高くでき、溶解性ＣＯＤＣｒ除去量を多くすることができる。 By the rapid detection of acid fermentation failure by the method of the present invention, by reducing the inflow organic matter load and / or increasing the residence time, even if acid fermentation failure occurs, the degradation of methane fermentation treatment performance is avoided, Furthermore, the methane-fermenting bacteria are not killed, the soluble COD Cr removal rate after inflow of the hardly fermentable substance can be made higher than that of the conventional method, and the soluble COD Cr removal amount can be increased.
本発明は、有機性廃水、特に比較的高分子の有機物や難発酵成分を含み、酸発酵工程が律速となる有機性廃水を対象として、酸発酵工程とメタン発酵工程からなら二相式嫌気性処理方式において、有機性廃水の有機物濃度検出手段及び流入量検出手段を設け、流入有機物負荷量あたりの酸発酵槽へのアルカリ剤注入量を指標として、酸発酵工程に注入されるアルカリ剤注入量の減少によって酸発酵不良を迅速に検知することで、流入有機物負荷量の変動に拘わらず、酸発酵不良を迅速に検知することで、メタン発酵処理性能の低下を回避するものである。
酸発酵不良の迅速な検知によって、流入有機物負荷量を減少且つ／又は滞留時間を増加させることで、酸発酵不良が発生してもメタン発酵処理性能の低下を回避し、さらにはメタン発酵菌を死滅させないことにある。
The present invention is intended for organic wastewater, particularly organic wastewater containing relatively high-molecular organic matter and difficult-to-ferment components, and rate-determining the acid fermentation process. In the treatment method, organic substance concentration detection means and inflow amount detection means are provided for organic wastewater, and the injection amount of alkaline agent injected into the acid fermentation process using the injection amount of alkaline agent into the acid fermenter per inflow organic matter load as an index By detecting acid fermentation failure quickly by reducing the amount of acid, the acid fermentation failure is detected quickly regardless of fluctuations in the inflowing organic matter load, thereby avoiding a decrease in methane fermentation treatment performance.
By detecting the acid fermentation failure quickly, reducing the inflowing organic matter load and / or increasing the residence time, it is possible to avoid degradation of methane fermentation treatment performance even if acid fermentation failure occurs, and There is in not letting you die.
以下、本発明の実施の形態を図面を参照して説明する。
本発明における嫌気性処理は、酸発酵を主に行う酸発酵槽と、メタン発酵を主に行うメタン発酵槽との２槽からなる二相式嫌気処理をいう。対象とする有機性廃水は、固形性成分を主とする泥状であっても、溶解性成分を主とする液状であってもよい。また、メタン発酵処理には、主に泥状の有機性廃水を嫌気処理する嫌気性消化法や、主に液状の有機性廃水を嫌気処理するＵＡＳＢ法、ＥＧＳＢ法、流動床法、固定床法などの高負荷嫌気性処理があるが、いずれの方式でも本発明に適用できる。
本発明の対象となる嫌気性処理は、３０℃〜３５℃を至適温度とした中温メタン発酵処理、５０℃〜５５℃を至適温度とした高温メタン発酵処理の温度範囲の嫌気性処理のいずれでもよい。
Hereinafter, embodiments of the present invention will be described with reference to the drawings.
The anaerobic treatment in the present invention refers to a two-phase anaerobic treatment comprising two tanks of an acid fermentation tank mainly for acid fermentation and a methane fermentation tank mainly for methane fermentation. The target organic waste water may be in the form of mud mainly composed of solid components or in the form of liquid mainly composed of soluble components. In addition, the methane fermentation treatment includes an anaerobic digestion method mainly for anaerobically treating mud organic wastewater, and a UASB method, an EGSB method, a fluidized bed method, a fixed bed method for anaerobically treating mainly liquid organic wastewater. However, any system can be applied to the present invention.
The anaerobic treatment that is the subject of the present invention is an anaerobic treatment in the temperature range of a medium temperature methane fermentation treatment with an optimum temperature of 30 ° C. to 35 ° C. and a high temperature methane fermentation treatment with an optimum temperature of 50 ° C. to 55 ° C. Either is acceptable.
図１及び図２は、嫌気性処理を実施するためにＵＡＳＢ法を例にした本発明の好ましい一形態の概要を例示した図である。図１は、メタン発酵工程流出水を循環しない例、図２は、メタン発酵工程流出水の一部を酸発酵工程に循環する例である。図２には、メタン発酵工程流出水の一部を循環水として酸発酵槽内部に返送するライン、及びメタン発酵工程流出水の一部をメタン発酵槽の流入部に返送するラインの両方が設置された図を一例として示した。
はじめに、メタン発酵工程流出水を循環しない例について、図１を用いて説明する。
食品工場、化学工場などの各種工場より排出され、難発酵成分の負荷変動がある有機性廃水を原水Ａとし、原水は、原水ポンプ１によって酸発酵槽２へ流入する。原水の流入水量は流量計３により測定される。流量は流量調節弁４で調節される。
FIG. 1 and FIG. 2 are diagrams illustrating an outline of a preferred embodiment of the present invention taking the UASB method as an example for performing anaerobic treatment. FIG. 1 is an example in which the methane fermentation process effluent is not circulated, and FIG. 2 is an example in which a part of the methane fermentation process effluent is circulated in the acid fermentation process. In Fig. 2, both a line for returning a part of the effluent from the methane fermentation process to the inside of the acid fermenter as circulating water and a line for returning a part of the effluent from the methane fermentation process to the inflow part of the methane fermenter are installed. The figure is shown as an example.
First, the example which does not circulate methane fermentation process effluent water is demonstrated using FIG.
Organic wastewater discharged from various factories such as food factories and chemical factories and having a load fluctuation of difficult-to-ferment components is used as raw water A, and the raw water flows into the acid fermentation tank 2 by the raw water pump 1. The amount of raw water inflow is measured by the flow meter 3. The flow rate is adjusted by the flow rate control valve 4.
酸発酵槽では、槽内の酸発酵菌の働きにより、炭水化物やたんぱく質、脂質などの複雑な有機化合物が、糖、アミノ酸、ペプチド等の単純な有機化合物に低分子化され、さらに長鎖脂肪酸、酢酸に分解される。
酸発酵槽では、有機酸の生成に伴いｐＨが低下するが、酸発酵に適したｐＨである５．０〜６．５とするために、酸発酵槽に設置されたｐＨ計５のｐＨ測定結果をもとに、所定ｐＨとなるようにアルカリ剤６をアルカリ剤添加ポンプ７にて注入する。アルカリ剤の注入量は、流量計８の積算により求められる。酸発酵槽のｐＨは酸発酵槽内にて測定してもよいし、酸発酵処理水Ｂを測定してもよい。アルカリ剤としては、ＮａＯＨ、Ｃａ（ＯＨ）２、Ｍｇ（ＯＨ）２、ＮａＨＣＯ３、Ｎａ２ＣＯ３などがあるが、ｐＨ制御の容易さ及び取り扱いの容易さを考慮して、ＮａＯＨを用いることが好ましい。
In acid fermentation tanks, complex organic compounds such as carbohydrates, proteins, and lipids are reduced to simple organic compounds such as sugars, amino acids, and peptides by the action of acid-fermenting bacteria in the tank. Decomposed into acetic acid.
In the acid fermenter, the pH decreases with the production of the organic acid, but the pH measurement of the pH meter 5 installed in the acid fermenter is performed in order to adjust the pH to 5.0 to 6.5, which is a pH suitable for acid fermentation. Based on the result, the alkaline agent 6 is injected by the alkaline agent addition pump 7 so as to obtain a predetermined pH. The injection amount of the alkaline agent is obtained by integrating the flow meter 8. The pH of the acid fermentation tank may be measured in the acid fermentation tank, or the acid fermentation treated water B may be measured. Examples of the alkaline agent include NaOH, Ca (OH) 2 , Mg (OH) 2 , NaHCO 3 , and Na 2 CO 3 , but use NaOH in consideration of ease of pH control and ease of handling. Is preferred.
アルカリ剤の注入位置は、酸発酵槽流入部、酸発酵槽内、メタン発酵処理水を酸発酵工程に循環を行う場合であればメタン発酵処理水循環配管のいずれでもよい。
また、原水が高ｐＨや低ｐＨの廃水である場合は酸又はアルカリを注入し、事前に中和を行うことが好ましい。
酸発酵槽で有機酸が生成された酸発酵処理水は、メタン発酵槽流入ポンプ９によって、メタン発酵槽１０へ流入される。
メタン発酵槽では、酢酸などの有機酸がメタン発酵菌によってメタンガスと二酸化炭素に分解されバイオガスとなる。バイオガスは、図示されていないガスラインによって系外に排出される。排出されたバイオガスは、必要に応じて脱硫等の処理を行った後、ボイラーや燃焼塔などへ送られ利用される。
The injection position of the alkaline agent may be any of the acid fermenter inflow part, the acid fermenter, and the methane fermentation treated water circulation pipe as long as the methane fermentation treated water is circulated in the acid fermentation process.
Moreover, when raw | natural water is wastewater of high pH or low pH, it is preferable to inject | pour an acid or an alkali and to neutralize in advance.
The acid fermentation treated water in which the organic acid is generated in the acid fermentation tank is flowed into the methane fermentation tank 10 by the methane fermentation tank inflow pump 9.
In a methane fermentation tank, an organic acid such as acetic acid is decomposed into methane gas and carbon dioxide by methane fermentation bacteria to become biogas. Biogas is discharged out of the system by a gas line (not shown). The discharged biogas is subjected to treatment such as desulfurization as necessary, and then sent to a boiler, a combustion tower or the like for use.
次に、メタン発酵工程流出水の一部を酸発酵工程に循環する例を、図２を用いて説明する。
メタン発酵工程流出水Ｃは、処理水Ｄとなるが、流出水の一部を酸発酵工程に循環する場合は、メタン発酵処理水を循環水Ｅとして、循環ポンプ１１によって酸発酵槽流入部あるいは酸発酵槽内部に返送する。循環水量は、流量計１２により測定される。流量は流量調節弁１３で調節される。
酸発酵工程ではアルカリ度を消費する酸発酵処理が、メタン発酵工程ではアルカリ度を生成するメタン発酵処理が進行するため、アルカリ度の高いメタン発酵処理水を酸発酵槽に循環することにより、メタン発酵工程で生成したアルカリ度を有効利用して、酸発酵槽に注入するアルカリ剤の使用量を削減できる。
Next, the example which circulates a part of methane fermentation process effluent water to an acid fermentation process is demonstrated using FIG.
The methane fermentation process effluent C becomes the treated water D, but when a part of the effluent is circulated to the acid fermentation process, the methane fermentation process water is used as the circulating water E by the circulation pump 11 or Return to the acid fermenter. The amount of circulating water is measured by the flow meter 12. The flow rate is adjusted by the flow rate control valve 13.
Since acid fermentation treatment that consumes alkalinity proceeds in the acid fermentation process, and methane fermentation treatment that produces alkalinity proceeds in the methane fermentation process, methane fermentation treated water with high alkalinity is circulated to the acid fermenter. It is possible to effectively use the alkalinity generated in the fermentation process and reduce the amount of the alkaline agent to be injected into the acid fermentation tank.
また、メタン発酵工程にＵＡＳＢ法、ＥＧＳＢ法、流動床法を採用した場合、循環水には、メタン発酵工程から後段の工程へ送られるメタン発酵処理水だけでなく、メタン発酵槽の汚泥界面上方に位置する中間部から直接引き抜いた槽内水を、メタン発酵工程流出水として用いることもできる。
さらに、メタン発酵工程にＵＡＳＢ法、ＥＧＳＢ法、流動床法を採用し、メタン発酵工程流出水の一部をメタン発酵工程に循環する場合は、メタン発酵槽の流入部やメタン発酵槽の底部や汚泥界面下方に位置する中間部に直接循環することがある。これにより、メタン発酵槽内のグラニュール汚泥や流動床の流動を促進でき、処理の安定化を図ることができる。したがって、メタン発酵工程流出水は、酸発酵工程への循環水と、メタン発酵工程への循環水と、後段の工程へ送られるメタン発酵工程処理水の合計となる。
In addition, when the UASB method, EGSB method, and fluidized bed method are adopted for the methane fermentation process, the circulating water includes not only the methane fermentation treated water sent from the methane fermentation process to the subsequent process but also the sludge interface above the methane fermentation tank. Water in the tank drawn directly from the intermediate part located in the methane fermentation process effluent can also be used.
Furthermore, when adopting UASB method, EGSB method, fluidized bed method for methane fermentation process and circulating part of effluent of methane fermentation process effluent to methane fermentation process, inflow part of methane fermenter, bottom of methane fermenter, It may circulate directly to the middle part located below the sludge interface. Thereby, the flow of the granular sludge in a methane fermentation tank and a fluidized bed can be accelerated | stimulated, and stabilization of a process can be aimed at. Therefore, the methane fermentation process outflow water is the sum of the circulating water to the acid fermentation process, the circulating water to the methane fermentation process, and the methane fermentation process treated water sent to the subsequent process.
原水の流入量と有機物濃度の積で表される有機物負荷が変動する場合、有機物負荷に応じて酸発酵工程で生成される有機酸量が増減し、有機酸量に応じてアルカリ剤注入量も増減することになる。本発明では、有機物負荷や有機酸生成量に応じたアルカリ剤注入量を指標とする。この場合、図１、図２に示すように、酸発酵槽へ流入する手前に有機物濃度計１４を設置し、有機物濃度のデータが制御装置１５へ送られ、制御装置において、式（１）によって算出される有機物負荷量あたりのアルカリ剤注入量の割合から算出されるアルカリ剤注入率を指標として、後述の制御を行う。特に、難発酵成分が一時的に原水に混入する状態が想定される場合に、有機物負荷あたりのアルカリ剤注入率を指標とすることが好ましい。難発酵成分が一時的に原水に混入した場合、酸発酵で生成される難発酵成分由来の有機酸量は少ないので、有機物負荷あたりのアルカリ剤注入率は減少することになる。
有機物負荷あたりのアルカリ剤注入率（ｋｇ／ｋｇ）
＝［アルカリ剤注入量（ｋｇ／ｄ）］÷［原水有機物濃度（ｋｇ／ｍ３）×原水量（ｍ３／ｄ）］ ・・・（１）
有機物濃度は、クロム酸カリウムによる化学的酸素要求量（ＣＯＤＣｒ；Ｃｈｅｍｉｃａｌ Ｏｘｙｇｅｎ Ｄｅｍａｎｄ）、全有機炭素（Ｔｏｔａｌ Ｏｒｇａｎｉｃ Ｃａｒｂｏｎ；ＴＯＣ）、全酸素要求量（Ｔｏｔａｌ Ｏｘｙｇｅｎ Ｄｅｍａｎｄ；ＴＯＤ）などいずれでもよい。
When the organic load expressed by the product of raw water inflow and organic substance concentration fluctuates, the amount of organic acid generated in the acid fermentation process increases or decreases depending on the organic load, and the amount of alkali agent injected depends on the amount of organic acid. Will increase or decrease. In the present invention, the amount of alkali agent injected according to the organic load and the amount of organic acid produced is used as an index. In this case, as shown in FIG. 1 and FIG. 2, the organic matter concentration meter 14 is installed before flowing into the acid fermenter, and the organic matter concentration data is sent to the control device 15. The below-described control is performed using the alkaline agent injection rate calculated from the ratio of the alkaline agent injection amount per calculated organic substance loading amount as an index. In particular, when it is assumed that a hardly fermentable component is temporarily mixed in raw water, it is preferable to use the alkali agent injection rate per organic substance load as an index. When the hardly fermentable component is temporarily mixed in the raw water, the amount of the organic acid derived from the difficultly fermented component produced by the acid fermentation is small, so that the alkali agent injection rate per organic substance load is decreased.
Alkaline agent injection rate per organic load (kg / kg)
= [Alkaline agent injection amount (kg / d)] ÷ [Raw water organic matter concentration (kg / m 3 ) × Raw water amount (m 3 / d)] (1)
The organic substance concentration may be any of chemical oxygen demand (COD Cr ; Chemical Oxygen Demand), total organic carbon (TOC), total oxygen demand (TOD), etc. due to potassium chromate.
図２に示すように、酸発酵工程にメタン発酵工程の処理水を循環水として戻す場合、循環水の水量とＭ−アルカリ度をそれぞれ流量計、Ｍ−アルカリ度計１６で測定し制御に組み込むことが好ましい。循環水の水量とＭ−アルカリ度を測定し制御に組み込むことで、循環水の影響を補正して酸発酵の状態を把握することができる。
この場合、制御装置では、式（２）によって算出されるアルカリ剤注入率を指標として用いる。なお、式（２）では、アルカリ剤注入量をＭ−アルカリ度換算した例を示したが、循環水のＭ−アルカリ度量をアルカリ剤量に換算してもよい。
有機物負荷あたりのアルカリ剤注入率（ｋｇ／ｋｇ）
＝［アルカリ剤注入量（Ｍ−アルカリ度換算）（ｋｇ／ｄ）
＋循環水Ｍ−アルカリ度量（ｋｇ／ｍ３）×循環水量（ｍ３／ｄ）］
÷［原水有機物濃度（ｋｇ／ｍ３）×原水量（ｍ３／ｄ）］ ・・・（２）
As shown in FIG. 2, when the treated water of the methane fermentation process is returned to the acid fermentation process as the circulating water, the amount of the circulating water and the M-alkalinity are measured by the flow meter and the M-alkaline meter 16 and incorporated in the control. It is preferable. By measuring the amount of circulating water and the M-alkalinity and incorporating it in the control, the influence of the circulating water can be corrected and the state of acid fermentation can be grasped.
In this case, the control device uses the alkaline agent injection rate calculated by the equation (2) as an index. In addition, in Formula (2), although the example which converted the alkaline agent injection amount into M-alkalinity was shown, you may convert the M-alkalinity amount of circulating water into the amount of alkaline agent.
Alkaline agent injection rate per organic load (kg / kg)
= [Alkaline agent injection amount (M-alkalinity conversion) (kg / d)
+ Circulating water M- alkali metric (kg / m 3) × circulating water (m 3 / d)]
÷ [Raw water organic matter concentration (kg / m 3 ) × Raw water amount (m 3 / d)] (2)
原水有機物濃度、循環水Ｍ−アルカリ度が安定している場合や、原水量、循環水量が一定の場合は、前記の式（１）、式（２）において、それぞれの値を入れて算出することができる。
制御装置にて算出された、式（１）、式（２）の有機物負荷あたりのアルカリ剤注入率の結果が設定値を下回った場合は、警報を発するとともに、１）原水量の減少あるいは停止、及び／又は、２）メタン発酵処理水の循環水量の減少あるいは停止する制御を行う。
図１、図２では、流量調整弁による流量調整の例を図示したが、流量を制御する方法はどのような方法でもよく、ポンプの回転数による制御でもよい。また、流量計によるアルカリ剤注入量の計測例を図示したが、アルカリ剤注入量を計測する方法はどのような方法でもよく、アルカリ剤貯留量の変化から注入量を求めてもよい。さらに、機器による測定と制御の例を示したが、手分析・手計算による制御も可能である。
When the raw water organic matter concentration and the circulating water M-alkalinity are stable, or when the raw water amount and the circulating water amount are constant, the respective values are calculated in the above formulas (1) and (2). be able to.
When the result of the alkaline agent injection rate per load of organic substances calculated by the control device is below the set value, an alarm is issued and 1) the amount of raw water is reduced or stopped And / or 2) Control to reduce or stop the amount of circulating water of methane fermentation treated water.
In FIGS. 1 and 2, an example of flow rate adjustment by the flow rate adjustment valve is illustrated, but any method may be used for controlling the flow rate, and control by the number of rotations of the pump may be used. Moreover, although the measurement example of the alkaline agent injection amount by the flow meter is illustrated, any method may be used for measuring the alkaline agent injection amount, and the injection amount may be obtained from a change in the alkaline agent storage amount. Furthermore, although the example of the measurement and control by an apparatus was shown, control by manual analysis and manual calculation is also possible.
前記の式（１）、式（２）にて算出されたアルカリ剤注入率による制御フローを図４に示す。
必要に応じて原水量、有機物濃度、循環水量、循環水のＭ−アルカリ度、アルカリ剤注入量を測定する（ａ）。測定結果を基に、式（１）あるいは式（２）より算出されるアルカリ剤注入率が算出される（ｂ）。
ｂにおいてアルカリ剤注入率が設定値以上であれば、酸発酵は良好との判定がなされ、一巡前の判定を参照する（ｃ）。一巡前の判定で、酸発酵が良好と判断されていれば、運転条件の変更は行われない（ｄ）。一巡前の判定で、酸発酵が不良と判断されていれば、一巡前に変更された原水量及び／又は循環水量の復帰を行う（ｅ）。
ｂにおいてアルカリ剤注入率が設定値未満であれば、酸発酵は不良との判定がなされ、一巡前の判定を参照する（ｆ）。一巡前の判定で、酸発酵が良好と判断されていれば、原水量の減少あるいは停止、及び／又は、循環水量の減少あるいは停止を行う（ｇ）。一巡前の判定で、酸発酵が不良と判断されていれば、運転条件の変更は行われない（ｈ）。
ｄ、ｅ、ｆ、ｇの後、制御を継続する場合はａへ戻る。
図４では、酸発酵不良の判定を一段階で行う例を説明したが、アルカリ剤注入率の設定値を２つ以上設けて、多段階で酸発酵不良を判定してもよい。
FIG. 4 shows a control flow based on the alkali agent injection rate calculated by the above formulas (1) and (2).
If necessary, the raw water amount, the organic matter concentration, the circulating water amount, the M-alkalinity of the circulating water, and the alkaline agent injection amount are measured (a). Based on the measurement result, the alkali agent injection rate calculated from the formula (1) or the formula (2) is calculated (b).
If the alkaline agent injection rate is equal to or greater than the set value in b, it is determined that the acid fermentation is good, and the determination before one round is referred to (c). If it is determined that the acid fermentation is good in the determination before one round, the operating condition is not changed (d). If it is determined that the acid fermentation is poor in the determination before one round, the raw water amount and / or the circulating water amount changed before the one round is restored (e).
If the alkaline agent injection rate is less than the set value in b, it is determined that the acid fermentation is defective, and the determination before one round is referred to (f). If it is determined that the acid fermentation is good in the determination before one round, the raw water amount is reduced or stopped and / or the circulating water amount is reduced or stopped (g). If it is determined that the acid fermentation is poor in the determination before one round, the operating condition is not changed (h).
After d, e, f, g, return to a to continue the control.
In FIG. 4, an example in which determination of acid fermentation failure is performed in one stage has been described, but two or more set values of the alkaline agent injection rate may be provided to determine acid fermentation failure in multiple stages.
アルカリ剤注入率の設定値は、循環水となるメタン発酵処理水由来のＭ−アルカリ度と供給アルカリ剤由来のアルカリ度とで供給される合計のＭ−アルカリ度が、中和処理後の原水のＴＯＣ １．０ｋｇ当たりのＭ−アルカリ度として０．３〜１．５ｋｇ、好ましくは０．６〜１．０ｋｇの間に設定される。
原水の受入停止もしくは原水量の低減を行う目的は、流入有機物負荷量を減少することで難発酵成分の負荷を減少させ、酸発酵工程で難発酵成分の酸発酵を、十分進めることができる。
原水の受入停止もしくは原水量の低減を行うこと、及びメタン発酵処理水の酸発酵工程への循環水量の低減もしくは停止を行う目的は、酸発酵工程における滞留時間を増加することにある。滞留時間を増加することにより、難発酵成分の酸発酵を十分進めることができる。
また、メタン発酵槽流入部への循環水量の低減もしくは停止を行うことにより、メタン発酵処理水中に残存する難発酵成分及び酸発酵が十分されていない難発酵成分を、メタン発酵槽に再流入させないことで、メタン発酵槽内での酸発酵の進行による槽内ｐＨの低下を抑制することもできる。
原水の流量の減少あるいは停止と、循環水量の減少あるいは停止の両方を行うことが好ましいが、受け入れなかった原水を産廃として工場外で処分することになり好ましくないので、循環水量の低減もしくは停止のみを行うこともできる。
The set value of the alkali agent injection rate is the total M-alkalinity supplied by the M-alkalinity derived from the methane fermentation treated water and the alkalinity derived from the supply alkaline agent as the circulating water. The M-alkalinity per 1.0 kg of TOC is set between 0.3 and 1.5 kg, preferably between 0.6 and 1.0 kg.
The purpose of stopping the acceptance of raw water or reducing the amount of raw water is to reduce the load of difficult-to-ferment components by reducing the inflow organic matter load, and to sufficiently promote acid fermentation of difficult-to-ferment components in the acid fermentation process.
The purpose of stopping acceptance of raw water or reducing the amount of raw water and reducing or stopping the amount of circulating water to the acid fermentation process of methane fermentation treated water is to increase the residence time in the acid fermentation process. By increasing the residence time, acid fermentation of difficult-to-ferment components can be sufficiently advanced.
In addition, by reducing or stopping the amount of circulating water to the methane fermentation tank inflow section, difficult fermentation components remaining in the methane fermentation treated water and difficult fermentation components with insufficient acid fermentation are not reflowed into the methane fermentation tank. Thereby, the fall of the pH in a tank by progress of acid fermentation in a methane fermentation tank can also be suppressed.
It is preferable to reduce or stop the flow of raw water and to reduce or stop the amount of circulating water, but it is not preferable because the unaccepted raw water is disposed of outside the factory as industrial waste. Can also be done.
以下に、本発明を実施例により従来法と共に、さらに具体的に説明する。
ＴＯＣ ３３００〜３７００ｍｇ／Ｌ、ＣＯＤＣｒ では９０００〜１００００ｍｇ／Ｌに調整した糖質系廃水を原水として、グラニュール汚泥を投入したＵＡＳＢタイプのメタン発酵槽で処理を行った。ＵＡＳＢの前段処理工程として酸発酵工程を設置し、酸発酵工程の設定ｐＨは６．０で運転した。アルカリ剤として水酸化ナトリウムを、無機栄養塩類として窒素、リンなどを添加した。水酸化ナトリウム １０００ｍｇ／ＬはＭ−アルカリ度 １２５０ｍｇ／Ｌとして換算することができる。種汚泥は、同じ清涼飲料廃水を処理している実機のグラニュール汚泥を投入した。有機物濃度としてＴＯＣを指標とした。本発明の制御を行う前の標準状態での原水量は２０Ｌ／ｄとした。このときＵＡＳＢのＣＯＤＣｒ容積負荷が２０ｋｇ／（ｍ３・ｄ）となる。なお、糖質系廃水のみの運転でＵＡＳＢのＣＯＤＣｒ容積負荷が３０ｋｇ／（ｍ３・ｄ）でも同等の処理が可能なことを事前に確認している。
In the following, the present invention will be described more specifically together with conventional methods by examples.
In TOC 3300-3700 mg / L, COD Cr was processed in a UASB type methane fermenter in which granule sludge was introduced using saccharide wastewater adjusted to 9000-10000 mg / L as raw water. An acid fermentation process was installed as a pre-treatment process of UASB, and the pH of the acid fermentation process was set at 6.0. Sodium hydroxide was added as an alkaline agent, and nitrogen, phosphorus, etc. were added as inorganic nutrients. Sodium hydroxide 1000 mg / L can be converted as M-alkalinity 1250 mg / L. For seed sludge, granule sludge of the actual machine treating the same soft drink wastewater was used. TOC was used as an index as the organic substance concentration. The amount of raw water in the standard state before performing the control of the present invention was 20 L / d. At this time, the COD Cr volumetric load of UASB is 20 kg / (m 3 · d). In addition, it has been confirmed in advance that the same treatment is possible even if the UASB COD Cr volumetric load is 30 kg / (m 3 · d) by operating only the sugar-based wastewater.
図１、図２、図３に示す二相式嫌気性排水処理装置にて運転を行った。酸発酵槽の有効容量は１０Ｌ、ＵＡＳＢ槽の有効容量は１０Ｌである。酸発酵槽及びＵＡＳＢ槽内部の水温は、３５℃に保たれるよう温度制御した。循環ありとした場合、ＵＡＳＢ処理水の一部を酸発酵槽もしくは、ＵＡＳＢ槽流入部に循環した。循環水量は２０Ｌ／ｄとした。
運転は、３０日間行い評価を行った。始めの１０日間は、Ｒｕｎ１とし糖質系廃水のみを原水として投入した。続く１０日間は、Ｒｕｎ２とし糖質系廃水に難発酵成分を混合した原水を投入した。難発酵成分として、Ａ系列、Ｄ系列、Ｅ系列ではマルチトール、Ｂ系列ではキシリトール、Ｃ系列ではデンプンを使用した。難発酵成分を混合した原水のＴＯＣは５２００〜５６００ｍｇ／Ｌ、ＣＯＤＣｒでは１４０００〜１５０００ｍｇ／Ｌとなり、難発酵成分はＴＯＣ、ＣＯＤＣｒの約３５％を占めた。最後の１０日間は、Ｒｕｎ３とし、Ｒｕｎ１と同じ糖質系廃水のみを原水として投入した。酸発酵状態の判定は、１日１回行った。
表１に運転条件を、表２に運転結果として各Ｒｕｎでの溶解性ＣＯＤＣｒ除去率の平均値、及びＲｕｎ２、Ｒｕｎ３の溶解性ＣＯＤＣｒ除去量を示す。図５には代表的な系列の処理結果の経時変化を示す。
ここで、
溶解性ＣＯＤＣｒ除去率（％）＝１００×（原水の溶解性ＣＯＤＣｒ濃度 − ＵＡＳＢ処理水の溶解性ＣＯＤＣｒ濃度）／原水の溶解性ＣＯＤＣｒ
原水及びＵＡＳＢ処理水の溶解性ＣＯＤＣｒ濃度（ｍｇ／Ｌ）は、孔径１．０μろ紙で得たろ液を分析し得た。
The operation was performed using the two-phase anaerobic wastewater treatment apparatus shown in FIGS. 1, 2, and 3. The effective capacity of the acid fermentation tank is 10L, and the effective capacity of the UASB tank is 10L. The water temperature inside the acid fermentation tank and the UASB tank was controlled to be kept at 35 ° C. When there was circulation, a part of the UASB treated water was circulated to the acid fermentation tank or the UASB tank inflow part. The amount of circulating water was 20 L / d.
The operation was performed for 30 days and evaluated. For the first 10 days, Run 1 was used as raw water and only saccharide wastewater was added. For the next 10 days, raw water mixed with a non-fermentable component in saccharide wastewater as Run 2 was added. As the hardly fermentable component, maltitol was used in the A series, D series, and E series, xylitol was used in the B series, and starch was used in the C series. The TOC of raw water mixed with difficult-to-ferment components was 5200 to 5600 mg / L, and COD Cr was 14,000 to 15000 mg / L, and the hardly-fermentable components accounted for about 35% of TOC and COD Cr . For the last 10 days, Run 3 was used, and only the same carbohydrate wastewater as Run 1 was used as raw water. The acid fermentation state was determined once a day.
The operating conditions are shown in Table 1, the average value of the solubility COD Cr removal rate for each Run as the operation results are shown in Table 2, and Run2, the solubility COD Cr removal of Run 3. FIG. 5 shows changes with time in the processing results of a typical series.
here,
Soluble COD Cr removal rate (%) = 100 × (soluble COD Cr concentration of the raw water - soluble COD Cr concentration of UASB treated water) / raw water solubility COD Cr
The solubility COD Cr concentration (mg / L) of raw water and UASB treated water was obtained by analyzing the filtrate obtained with a filter paper having a pore size of 1.0 μm.
次に各系列の運転条件及び結果について、詳細に説明する。
Ａ−１系列（従来法）
従来法のＡ−１系列は、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
Ａ−１系列では、原水量２０Ｌ／ｄ、循環水量２０Ｌ／ｄの一定条件とし、流入有機物負荷量による酸発酵状態の判定は行わなかった。
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定した処理が行えていたが、Ｒｕｎ２になるとアルカリ剤注入量が減少すると共に、溶解性ＣＯＤＣｒ除去率の平均値は２７％に低下した。
Ｒｕｎ３においても、溶解性ＣＯＤＣｒ除去率は改善せず、溶解性ＣＯＤＣｒ除去率の平均値は５％と著しく低かった。
Next, the operating conditions and results of each series will be described in detail.
A-1 series (conventional method)
The conventional method A-1 series was processed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Maltitol was used as a difficult-to-ferment component.
In the A-1 series, the conditions of the raw water amount 20 L / d and the circulating water amount 20 L / d were set as constant conditions, and the acid fermentation state was not determined based on the inflowing organic matter load.
In Run 1, stable treatment could be performed with an average value of 88% of the soluble COD Cr removal rate. However, when Run 2 was reached, the amount of alkali agent injected was reduced and the average value of the soluble COD Cr removal rate was reduced to 27%. did.
Also in Run 3, the soluble COD Cr removal rate did not improve, and the average value of the soluble COD Cr removal rate was extremely low at 5%.
Ａ−２系列（従来法）
従来法のＡ−２系列は、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
Ａ−２系列では、ＵＡＳＢ処理水に残存する有機酸量が設定値を超えたと判断した場合にメタン発酵不良状態と判定して原水量を減少させる制御を行った。すなわちＴＯＣ負荷あたりのアルカリ剤注入率が０．７ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣを超えた場合にメタン発酵不良状態と判定し、原水の受入量を５０％にすることにした。その後、ＴＯＣ負荷あたりのアルカリ剤注入率が０．７ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣより下がった場合にメタン発酵状態が改善したと判定し、原水量を元に戻すこととした。
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定して処理が行えていた。Ｒｕｎ２の３日後、アルカリ剤注入率が０．７３ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなりメタン発酵不良状態と判定されたため、原水受入量を２０Ｌ／ｄから１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は３２％であった。Ｒｕｎ３のＴＯＣあたりのアルカリ剤注入量は設定値を超えて維持され、メタン発酵状態の改善を示すアルカリ注入率に到達しなかったので原水量も元に戻さなかった。その結果、Ｒｕｎ３の溶解性ＣＯＤＣｒ除去率の平均値は３０％と低かった。
A-2 series (conventional method)
The conventional method A-2 series was processed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Maltitol was used as a difficult-to-ferment component.
In the A-2 series, when it was determined that the amount of organic acid remaining in the UASB treated water exceeded the set value, it was determined that the methane fermentation was in a poor state, and control was performed to reduce the amount of raw water. That is, when the alkali agent injection rate per TOC load exceeded 0.7 kg-M alkalinity / kg-TOC, it was determined that the methane fermentation was in a poor state, and the amount of raw water received was 50%. After that, when the alkali agent injection rate per TOC load was lower than 0.7 kg-M alkalinity / kg-TOC, it was determined that the methane fermentation state had improved, and the raw water amount was returned to the original.
In Run 1, the treatment was stably performed with an average value of 88% for the removal rate of soluble COD Cr . Three days after Run 2, the alkaline agent injection rate was 0.73 kg-M alkalinity / kg-TOC, and the methane fermentation was judged to be in a poor state, so the amount of raw water received was reduced from 20 L / d to 10 L / d. The average value of Run2 soluble COD Cr removal rate was 32%. The amount of alkaline agent injected per TOC of Run 3 was maintained beyond the set value, and the amount of raw water was not restored because it did not reach the alkali injection rate indicating an improvement in the methane fermentation state. As a result, the average value of the soluble COD Cr removal rate of Run 3 was as low as 30%.
Ａ−３系列（従来法）
従来法のＡ−３系列は、図３に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。メタン発酵工程で発生するバイオガスのガス流量計１７、メタン濃度計１８を設置した。難発酵成分としてマルチトールを使用した。
原水量、原水ＴＯＣ、メタンガス発生量を測定し、ＴＯＣ負荷量あたりのメタンガス発生量から算出されるＴＯＣ負荷あたりのガス化率を式（３）により算出した。メタン発酵不良と判定するＴＯＣ負荷あたりのガス化率の制御設定値を０．７５ｍ３−メタンガス（ＮＴＰ）／ｋｇ−原水ＴＯＣとした。Ａ−３系列ではＴＯＣ負荷あたりのガス化率が設定値未満に減少した場合にメタン発酵不良と判定した。その後、ＴＯＣ負荷あたりのガス化率が増加した場合にメタン発酵状態が改善したと判定し、原水量を元に戻すこととした。
ＴＯＣ負荷あたりのガス化率［ｍ３−メタンガス（ＮＴＰ）／ｋｇ−原水ＴＯＣ］
＝［メタンガス発生量［ｍ３−メタンガス（ＮＴＰ）／ｄ］
÷［原水ＴＯＣ濃度（ｋｇ／ｍ３）×原水量（ｍ３／ｄ）］ ・・・（３）
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定した処理が行えていた。Ｒｕｎ２の２日後になるとガス化率は設定値未満の０．７２ｍ３−メタンガス（ＮＴＰ）／ｋｇ−原水ＴＯＣに減少したため、原水受入量を１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は５０％となった。Ｒｕｎ３のガス化率は設定値未満で、Ｒｕｎ３の溶解性ＣＯＤＣｒ除去率の平均値は４５％であった。
A-3 series (conventional method)
The conventional method A-3 series was processed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. A gas flow meter 17 and a methane concentration meter 18 for biogas generated in the methane fermentation process were installed. Maltitol was used as a difficult-to-ferment component.
The raw water amount, raw water TOC, and methane gas generation amount were measured, and the gasification rate per TOC load calculated from the methane gas generation amount per TOC load amount was calculated by Equation (3). The control set value of the gasification rate per TOC load determined to be methane fermentation failure was set to 0.75 m 3 -methane gas (NTP) / kg-raw water TOC. In the A-3 series, when the gasification rate per TOC load decreased below the set value, it was determined that the methane fermentation was poor. Then, when the gasification rate per TOC load increased, it was determined that the state of methane fermentation was improved, and the amount of raw water was restored.
Gasification rate per TOC load [m 3 -methane gas (NTP) / kg-raw water TOC]
= [Methane gas generation amount [m 3 -methane gas (NTP) / d]
÷ [Raw water TOC concentration (kg / m 3 ) × Raw water amount (m 3 / d)] (3)
In Run 1, stable treatment was possible with an average value of 88% for the removal rate of soluble COD Cr . Two days after Run 2, the gasification rate was reduced to 0.72 m 3 -methane gas (NTP) / kg-raw water TOC, which was less than the set value, so the raw water acceptance amount was reduced to 10 L / d. The average value of Run2 soluble COD Cr removal rate was 50%. The gasification rate of Run 3 was less than the set value, and the average value of Run 3 soluble COD Cr removal rate was 45%.
Ａ−４系列（本発明）
本発明のＡ−４系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は、循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ａ−４系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水量を７５％の１５Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、原水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．５４ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、原水量を１５Ｌ／ｄに減少した。Ｒｕｎ２では溶解性ＣＯＤＣｒ除去率の平均値は５２％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．８４ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり、酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は７７％となった。
本発明の方法により、難発酵物質流入時に一時的に処理が悪化したものの、従来法Ａ−２系列、Ａ−３系列より迅速に酸発酵不良を検知することができ、従来法Ａ−１系列、Ａ−２系列、Ａ−３系列より、適正な負荷とすることでＲｕｎ２、Ｒｕｎ３での除去溶解性ＣＯＤＣｒ量は多かった。
A-4 series (present invention)
In the A-4 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermenter as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the A-4 series, when it decreased below this control setting, it was determined that acid fermentation was poor.
When it was determined that the acid fermentation state was poor, the raw water amount was 75% of 15 L / d. When it was determined that the acid fermentation state was recovered, the raw water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate became 0.54 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The raw water amount was reduced to 15 L / d. In Run 2, the average value of the soluble COD Cr removal rate was 52%. One day after Run 3, the alkaline agent injection rate was 0.84 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered. The average value of the soluble COD Cr removal rate was 77%.
According to the method of the present invention, although the treatment is temporarily deteriorated when the hardly fermentable substance flows in, the acid fermentation failure can be detected more quickly than the conventional methods A-2 series and A-3 series, and the conventional method A-1 series From the A-2 series and A-3 series, the amount of removed soluble COD Cr in Run 2 and Run 3 was higher by setting the load appropriately.
Ａ−５系列（本発明）
本発明のＡ−５系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は、循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ａ−５系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水量を５０％の１０Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、原水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．４７ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、原水量を１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は８５％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．８８ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。
本発明の方法により、難発酵物質流入時に一時的に処理が悪化したものの、従来法Ａ−２系列、Ａ−３系列より迅速に酸発酵不良を検知することができ、本願発明のＡ−４系列と比べてさらに安定した処理が可能であり、適正な負荷とすることでＲｕｎ２、Ｒｕｎ３での除去溶解性ＣＯＤＣｒ量は多かった。
A-5 series (present invention)
In the A-5 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermenter as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the A-5 series, it was determined that acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the amount of raw water was 50% of 10 L / d. When it was determined that the acid fermentation state was recovered, the raw water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate became 0.47 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of raw water was reduced to 10 L / d. The average value of the soluble CODCr removal rate of Run 2 was 85%. One day after Run 3, the alkaline agent injection rate was 0.88 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered. The average value of the soluble CODCr removal rate was 88%.
By the method of the present invention, although the treatment was temporarily deteriorated when the hardly fermentable substance flowed in, the acid fermentation failure could be detected more quickly than the conventional methods A-2 series and A-3 series. More stable treatment was possible compared to the series, and the removal soluble COD Cr amount in Run 2 and Run 3 was large by setting the load appropriately.
Ａ−６系列（本発明）
本発明のＡ−６系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ａ−６系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水の供給を停止した。原水の供給を停止しているため、アルカリ剤注入が停止した時点を酸発酵状態が回復したと判定し、原水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．４７ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり、酸発酵不良と判定されたため、原水の供給を停止した。Ｒｕｎ２では、１日おきに酸発酵状態の不良と良好の判定を繰り返し、溶解性ＣＯＤＣｒ除去率の平均値は８４％となった。Ｒｕｎ３の１日後には、酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。
本発明の方法によるＴＯＣ負荷あたりのアルカリ剤注入率が設定値以下に減少した場合に原水の受入停止を行う制御により、適正な負荷とすることで安定した処理が可能であった。
A-6 series (present invention)
In the A-6 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the A-6 series, it was determined that acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the supply of raw water was stopped. Since the supply of raw water was stopped, it was determined that the acid fermentation state had recovered when the alkaline agent injection was stopped, and the raw water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkali agent injection rate became 0.47 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The supply of raw water was stopped. In Run 2, the acid fermentation state was determined to be poor and good every other day, and the average value of the soluble COD Cr removal rate was 84%. One day after Run3, it was determined that the acid fermentation state had recovered, so the amount of water was returned to the original amount. The average value of the soluble COD Cr removal rate was 88%.
When the alkaline agent injection rate per TOC load according to the method of the present invention is reduced to a set value or less, stable treatment can be performed by setting an appropriate load by controlling to stop receiving raw water.
Ａ−７系列（本発明）
本発明のＡ−７系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は、循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ａ−７系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、循環水量を５０％の１０Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、循環水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．５７ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、循環水量を１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は７２％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．７３ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８６％となった。
本発明の方法により、適正な酸発酵槽の滞留時間を確保し、処理水中の難発酵成分の再流入を低減することで安定した処理が可能であった。
A-7 series (present invention)
In the A-7 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermenter as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the A-7 series, it was determined that acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the amount of circulating water was 50%, 10 L / d. When it was determined that the acid fermentation state was recovered, the circulating water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkali agent injection rate became 0.57 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of circulating water was reduced to 10 L / d. The average value of the soluble COD Cr removal rate of Run 2 was 72%. One day after Run 3, the alkaline agent injection rate became 0.73 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered. The average value of the soluble COD Cr removal rate was 86%.
By the method of the present invention, a stable treatment was possible by securing a proper residence time of the acid fermenter and reducing reflow of difficult-to-ferment components in the treated water.
Ａ−８系列（本発明）
本発明のＡ−８系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ａ−８系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、循環水の供給を停止した。酸発酵状態が回復したと判定された場合、循環水の供給を再開した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．５８ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、循環水の供給を停止した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は７６％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．６５ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、循環水の供給を再開した。溶解性ＣＯＤＣｒ除去率の平均値は８７％となった。
本発明の方法により、適正な酸発酵槽の滞留時間を確保し、処理水中の難発酵成分の再流入を低減することで安定した処理が可能であった。
A-8 series (present invention)
In the A-8 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the A-8 series, it was determined that acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the supply of circulating water was stopped. When it was determined that the acid fermentation state was recovered, the supply of circulating water was resumed.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate was 0.58 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The supply of circulating water was stopped. The average value of the run-off soluble COD Cr removal rate was 76%. One day after Run 3, the alkaline agent injection rate was 0.65 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered, so the supply of circulating water was resumed. The average value of the soluble COD Cr removal rate was 87%.
By the method of the present invention, a stable treatment was possible by securing a proper residence time of the acid fermenter and reducing reflow of difficult-to-ferment components in the treated water.
Ａ−９系列（本発明）
本発明のＡ−９系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ａ−９系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水量を５０％の１０Ｌ／ｄとすると共に、循環水量を５０％の１０Ｌ／ｄとした。酸発酵状態が回復したと判定された場合、原水量及び循環水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．５４ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、原水量と循環水量を５０％に減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．８１ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、循環水の供給を再開した。溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。
本発明の方法により、適正な負荷及び適正な酸発酵槽の滞留時間を確保し、処理水中の難発酵成分の再流入を低減することで安定した処理が可能であった。
A-9 series (present invention)
In the A-9 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the A-9 series, it was determined that acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the raw water amount was 50% 10 L / d and the circulating water amount was 50% 10 L / d. When it was determined that the acid fermentation state was recovered, the raw water amount and the circulating water amount were returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate became 0.54 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of raw water and circulating water was reduced to 50%. The average value of Run2 soluble COD Cr removal rate was 88%. One day after Run 3, the alkaline agent injection rate was 0.81 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered, so the supply of circulating water was resumed. The average value of the soluble COD Cr removal rate was 88%.
According to the method of the present invention, it was possible to ensure a proper load and a proper residence time of the acid fermenter, and to reduce the reflow of difficult-to-ferment components in the treated water, thereby enabling stable treatment.
Ｂ−１系列（従来法）
従来法のＢ−１系列は、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてキシリトールを使用した。
Ｂ−１系列では、原水量２０Ｌ／ｄ、循環水量２０Ｌ／ｄの一定条件とし、酸発酵状態の判定は行わなかった。
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定した処理が行えていたが、Ｒｕｎ２になるとアルカリ剤注入量が減少すると共に、溶解性ＣＯＤＣｒ除去率の平均値は２８％に低下した。
Ｒｕｎ３においても、溶解性ＣＯＤＣｒ除去率は改善せず、溶解性ＣＯＤＣｒ除去率の平均値は５％と著しく低かった。
B-1 series (conventional method)
The B-1 series of the conventional method was processed with the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Xylitol was used as a difficult-to-ferment component.
In the B-1 series, the raw water amount was 20 L / d and the circulating water amount was 20 L / d, and the acid fermentation state was not determined.
In Run 1, stable treatment could be performed with an average value of 88% of the soluble COD Cr removal rate. However, when Run 2 was reached, the alkaline agent injection amount decreased and the average value of the soluble COD Cr removal rate dropped to 28%. did.
Also in Run 3, the soluble COD Cr removal rate did not improve, and the average value of the soluble COD Cr removal rate was extremely low at 5%.
Ｂ−２系列（本発明）
本発明のＢ−２系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてキシリトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ｂ−２系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水量を５０％の１０Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、原水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．５５ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、原水量を１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は８５％となった。Ｒｕｎ３の１日後にはアルカリ剤注入率が０．８９ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。
本発明の方法により、難発酵物質流入時に一時的に処理が悪化したものの、従来法Ｂ−２系列より、適正な負荷とすることでＲｕｎ２、Ｒｕｎ３での除去溶解性ＣＯＤＣｒ量は多かった。
B-2 series (present invention)
In the B-2 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Xylitol was used as a difficult-to-ferment component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the B-2 series, it was determined that acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the amount of raw water was 50% of 10 L / d. When it was determined that the acid fermentation state was recovered, the raw water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate was 0.55 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of raw water was reduced to 10 L / d. The average value of the run-off soluble COD Cr removal rate was 85%. One day after Run 3, the alkaline agent injection rate was 0.89 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered. The average value of the soluble COD Cr removal rate was 88%.
Although the treatment temporarily deteriorated when the difficult-to-ferment substance flowed in by the method of the present invention, the amount of removed soluble COD Cr in Run 2 and Run 3 was larger than in the conventional method B-2 series by setting an appropriate load.
Ｃ−１系列（従来法）
従来法のＣ−１系列は、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてデンプンを使用した。
Ｃ−１系列では、原水量２０Ｌ／ｄ、循環水量２０Ｌ／ｄの一定条件とし、酸発酵状態の判定は行わなかった。
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定した処理が行えていたが、Ｒｕｎ２になるとアルカリ剤注入量が減少すると共に、溶解性ＣＯＤＣｒ除去率の平均値は４２％に低下した。
Ｒｕｎ３においても、溶解性ＣＯＤＣｒ除去率は改善せず、溶解性ＣＯＤＣｒ除去率の平均値は３０％と低かった。
C-1 series (conventional method)
The C-1 series of the conventional method was processed with the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Starch was used as a hardly fermentable component.
In the C-1 series, the raw water amount was 20 L / d and the circulating water amount was 20 L / d, and the acid fermentation state was not determined.
In Run 1, stable treatment was performed with an average value of 88% soluble COD Cr removal rate. However, when Run 2 was reached, the amount of alkali agent injected decreased and the average value of soluble COD Cr removal rate dropped to 42%. did.
Also in Run 3, the soluble COD Cr removal rate did not improve, and the average value of the soluble COD Cr removal rate was as low as 30%.
Ｃ−２系列（本発明）
本発明のＣ−２系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水として酸発酵槽に戻した。難発酵成分としてデンプンを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣ、循環水量、循環水のアルカリ度を測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（２）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ｃ−２系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水量を５０％の１０Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、原水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．５８ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、原水量を１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．９３ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。
本発明の方法により、従来法Ｃ−１系列より、適正な負荷とすることでＲｕｎ２、Ｒｕｎ３での除去溶解性ＣＯＤＣｒ量は多かった。
C-2 series (present invention)
In the C-2 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the acid fermentation tank as circulating water. Starch was used as a hardly fermentable component.
The alkali agent injection amount, the raw water amount, the raw water TOC, the circulating water amount, and the alkalinity of the circulating water in the acid fermenter were measured, and the alkali agent injection rate per TOC load was calculated by the formula (2). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the C-2 series, it was determined that the acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the amount of raw water was 50% of 10 L / d. When it was determined that the acid fermentation state was recovered, the raw water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate was 0.58 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of raw water was reduced to 10 L / d. The average value of Run2 soluble COD Cr removal rate was 88%. One day after Run 3, the alkaline agent injection rate was 0.93 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered. The average value of the soluble COD Cr removal rate was 88%.
By the method of the present invention, the amount of removed soluble COD Cr in Run 2 and Run 3 was higher than in the conventional method C-1 series by setting the load appropriately.
Ｄ−１系列（従来法）
従来法のＤ−１系列では、図１に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の循環は行わなかった。難発酵成分としてマルチトールを使用した。
Ｄ−１系列では、原水量２０Ｌ／ｄの一定条件とし、酸発酵状態の判定は行わなかった。
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定した処理が行えていたが、Ｒｕｎ２になるとアルカリ剤注入量が減少すると共に、溶解性ＣＯＤＣｒ除去率の平均値は６９％に低下した。
Ｒｕｎ３の溶解性ＣＯＤＣｒ除去率の平均値は８３％であった。
D-1 series (conventional method)
In the conventional method D-1 series, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. The UASB treated water was not circulated. Maltitol was used as a difficult-to-ferment component.
In D-1 series, it was set as the fixed conditions of the raw water amount 20L / d, and the acid fermentation state was not determined.
In Run 1, stable treatment was possible with an average value of 88% soluble COD Cr removal rate, but with Run 2, the amount of alkali agent injected decreased and the average value of soluble COD Cr removal rate dropped to 69%. did.
The average removal rate of the soluble CODCr of Run3 was 83%.
Ｄ−２系列（本発明）
本発明のＤ−２系列では、図１に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の循環は行わなかった。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣを測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（１）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ｄ−２系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、原水量を７５％の１５Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、原水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．４９ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、循環水量を１５Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．８１ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、元の水量に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８８％となった。
本発明の方法により、Ｄ−１系列と比べて適正な負荷とすることでことで安定した処理が可能であった。Ｄ−１系列、Ｄ−２系列では、循環がないため酸発酵槽の滞留時間が長く、Ａ−８系列の酸発酵不良時の運転に相当するため、処理性能の低下は少なかったが、Ａ−８系列と比べてアルカリ剤注入量が多くなった。
D-2 series (present invention)
In the D-2 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. The UASB treated water was not circulated. Maltitol was used as a difficult-to-ferment component.
The alkaline agent injection amount, raw water amount, and raw water TOC in the acid fermenter were measured, and the alkaline agent injection rate per TOC load was calculated by equation (1). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In the D-2 series, it was determined that the acid fermentation was poor when it decreased below this control setting.
When it was determined that the acid fermentation state was poor, the raw water amount was 75% of 15 L / d. When it was determined that the acid fermentation state was recovered, the raw water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate became 0.49 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of circulating water was reduced to 15 L / d. The average value of Run2 soluble COD Cr removal rate was 88%. One day after Run 3, the alkaline agent injection rate was 0.81 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered. The average value of the soluble COD Cr removal rate was 88%.
By the method of the present invention, stable processing was possible by setting the load appropriately as compared with the D-1 series. In the D-1 series and D-2 series, since there is no circulation, the residence time of the acid fermenter is long, and it corresponds to the operation at the time of poor acid fermentation of the A-8 series. Compared with the -8 series, the amount of alkali agent injected was increased.
Ｅ−１系列（従来法）
従来法のＥ−１系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水としてＵＡＳＢ流入部に戻した。難発酵成分としてマルチトールを使用した。
Ｅ−１系列では、原水量２０Ｌ／ｄ、循環水量２０Ｌ／ｄの一定条件とし、酸発酵状態の判定は行わなかった。
Ｒｕｎ１では、溶解性ＣＯＤＣｒ除去率の平均値８８％で安定した処理が行えていたが、Ｒｕｎ２になるとアルカリ剤注入量が減少すると共に、溶解性ＣＯＤＣｒ除去率の平均値は５８％に低下した。
Ｒｕｎ３の溶解性ＣＯＤＣｒ除去率の平均値は７０％であった。
E-1 series (conventional method)
In the E-1 series of the conventional method, it processed with the two-phase type anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the UASB inflow part as circulating water. Maltitol was used as a difficult-to-ferment component.
In the E-1 series, the raw water amount was 20 L / d and the circulating water amount was 20 L / d, and the acid fermentation state was not determined.
In Run 1, stable treatment could be performed with an average value of 88% soluble COD Cr removal rate, but with Run 2, the amount of alkali agent injected decreased and the average value of soluble COD Cr removal rate decreased to 58%. did.
The average value of Run3 soluble COD Cr removal rate was 70%.
・Ｅ−２系列（本発明）
本発明のＥ−２系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水としてＵＡＳＢ流入部に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣを測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（１）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ｅ−２系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、循環水量を５０％の１０Ｌ／ｄにした。酸発酵状態が回復したと判定された場合、循環水量を元の水量に戻した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．４９ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、循環水量を１０Ｌ／ｄに減少した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は６６％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．６９ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、循環水量を元に戻した。溶解性ＣＯＤＣｒ除去率の平均値は８６％となった。
本発明の方法により、適正な酸発酵槽の滞留時間を確保し、処理水中の難発酵成分の再流入を低減することで安定した処理が可能であった。
E-2 series (present invention)
In the E-2 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the UASB inflow part as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkaline agent injection amount, raw water amount, and raw water TOC in the acid fermenter were measured, and the alkaline agent injection rate per TOC load was calculated by equation (1). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In E-2 series, when it decreased to less than this control setting, it determined with acid fermentation failure.
When it was determined that the acid fermentation state was poor, the amount of circulating water was 50%, 10 L / d. When it was determined that the acid fermentation state was recovered, the circulating water amount was returned to the original water amount.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate became 0.49 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The amount of circulating water was reduced to 10 L / d. The average value of the soluble COD Cr removal rate of Run2 was 66%. One day after Run 3, the alkaline agent injection rate was 0.69 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered, so the amount of circulating water was restored. The average value of the soluble COD Cr removal rate was 86%.
By the method of the present invention, a stable treatment was possible by securing a proper residence time of the acid fermenter and reducing reflow of difficult-to-ferment components in the treated water.
Ｅ−３系列（本発明）
本発明のＥ−３系列では、図２に示す二相式嫌気性排水処理装置にて処理を行った。ＵＡＳＢ処理水の一部は循環水としてＵＡＳＢ流入部に戻した。難発酵成分としてマルチトールを使用した。
酸発酵槽でのアルカリ剤注入量、原水量、原水ＴＯＣを測定し、ＴＯＣ負荷あたりのアルカリ剤注入率を式（１）により算出した。酸発酵不良と判定するＴＯＣ負荷あたりのアルカリ剤注入率の制御設定値を０．６ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとした。Ｅ−３系列では、本制御設定未満に減少した場合に酸発酵不良と判定した。
酸発酵状態が不良と判定された場合、循環水の供給を停止した。酸発酵状態が回復したと判定された場合、循環水の供給を再開した。
Ｒｕｎ１では、平均ＣＯＤＣｒ除去率８８％で安定した処理が行えていたが、Ｒｕｎ２の１日後、アルカリ剤注入率が０．４９ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵不良と判定されたため、循環水の供給を停止した。Ｒｕｎ２の溶解性ＣＯＤＣｒ除去率の平均値は７７％となった。Ｒｕｎ３の１日後には、アルカリ剤注入率が０．６９ｋｇ−Ｍアルカリ度／ｋｇ−ＴＯＣとなり酸発酵状態は回復したと判定されたため、循環水の供給を再開した。溶解性ＣＯＤＣｒ除去率の平均値は８７％となった。
本発明の方法により、適正な酸発酵槽の滞留時間を確保し、処理水中の難発酵成分の再流入を低減することで安定した処理が可能であった。
E-3 series (present invention)
In the E-3 series of the present invention, the treatment was performed by the two-phase anaerobic waste water treatment apparatus shown in FIG. A part of the UASB treated water was returned to the UASB inflow part as circulating water. Maltitol was used as a difficult-to-ferment component.
The alkaline agent injection amount, raw water amount, and raw water TOC in the acid fermenter were measured, and the alkaline agent injection rate per TOC load was calculated by equation (1). The control set value of the alkali agent injection rate per TOC load determined to be acid fermentation failure was 0.6 kg-M alkalinity / kg-TOC. In E-3 series, when it decreased to less than this control setting, it determined with acid fermentation failure.
When it was determined that the acid fermentation state was poor, the supply of circulating water was stopped. When it was determined that the acid fermentation state was recovered, the supply of circulating water was resumed.
In Run 1, stable treatment could be performed with an average COD Cr removal rate of 88%, but one day after Run 2, the alkaline agent injection rate became 0.49 kg-M alkalinity / kg-TOC, and it was determined that acid fermentation was poor. The supply of circulating water was stopped. The average value of Run2 soluble COD Cr removal rate was 77%. One day after Run 3, the alkaline agent injection rate was 0.69 kg-M alkalinity / kg-TOC, and it was determined that the acid fermentation state had recovered, so the supply of circulating water was resumed. The average value of the soluble COD Cr removal rate was 87%.
By the method of the present invention, a stable treatment was possible by securing a proper residence time of the acid fermenter and reducing reflow of difficult-to-ferment components in the treated water.
１：原水ポンプ、２：酸発酵槽、３、８、１２：流量計、４、１３：流量調節弁、５：ｐＨ計、６：アルカリ剤、７：アルカリ剤添加ポンプ、９：メタン発酵槽流入ポンプ、１０：メタン発酵槽、１１：循環ポンプ、１４：有機物濃度計、１５：制御装置、１６：アルカリ度計、１７：ガス流量計、１８：メタンガス濃度計 1: Raw water pump, 2: Acid fermenter, 3, 8, 12: Flow meter, 4, 13: Flow control valve, 5: pH meter, 6: Alkaline agent, 7: Alkaline agent addition pump, 9: Methane fermenter Inflow pump, 10: methane fermenter, 11: circulation pump, 14: organic substance concentration meter, 15: control device, 16: alkalinity meter, 17: gas flow meter, 18: methane gas concentration meter
Claims (8)
The path for circulating the effluent of the methane fermenter has a flow rate control means for controlling the circulation amount of the effluent, and the alkaline agent injection rate determined from the injection amount of the alkaline agent and the organic substance load amount. The anaerobic treatment apparatus according to claim 7, further comprising a mechanism for controlling a circulation amount of the circulating water based on the set value.
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