JP2005185967A - Treatment method and treatment apparatus for organic waste water - Google Patents

Treatment method and treatment apparatus for organic waste water Download PDF

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JP2005185967A
JP2005185967A JP2003430983A JP2003430983A JP2005185967A JP 2005185967 A JP2005185967 A JP 2005185967A JP 2003430983 A JP2003430983 A JP 2003430983A JP 2003430983 A JP2003430983 A JP 2003430983A JP 2005185967 A JP2005185967 A JP 2005185967A
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organic wastewater
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Haruyuki Chiku
治之 知久
Hideki Inaba
英樹 稲葉
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Sumitomo Heavy Industries Ltd
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Abstract

<P>PROBLEM TO BE SOLVED: To provide a treatment method capable of highly treating even organic waste water containing sulfate ion or sulfite ion. <P>SOLUTION: The treatment method includes a 1st step for carrying out an acid formation treatment of the organic waste water containing sulfate ion and/or sulfite ion and for reducing the sulfate ion and/or sulfite ion to form sulfide, a 2nd step for adding an iron salt based inorganic flocculant into the organic waste water obtained by the 1st step and containing the sulfide to flocculate the sulfide to be separated from the organic water water and a 3rd step for anaerobically treating the organic waste water which is obtained in the 2nd step and from which the sulfide is separated. The methane fermentation of organic components in the organic waste water is smoothly carried out in the anaerobic treatment because the sulfate ion and the sulfite ion are removed from the organic waste water before the anaerobic treatment. <P>COPYRIGHT: (C)2005,JPO&NCIPI

Description

本発明は、有機性廃水の処理方法及び装置、特に硫酸イオン（ＳＯ４ ２−）や亜硫酸イオン（ＳＯ３ ２−）を含む有機性廃水を処理する処理方法に関する。 The present invention relates to a method and apparatus for treating organic wastewater, and more particularly to a treatment method for treating organic wastewater containing sulfate ions (SO 4 2− ) and sulfite ions (SO 3 2− ).

工場等からの廃水のような有機性廃水の処理においては、嫌気性処理のうちグラニュール（例えばグラニュールメタン菌）を利用するＵＡＳＢ式(Upflow Anaerobic Sludge Blanket：上向流嫌気性汚泥床式）或いはＥＧＡＢ式（Expanded Granular Sludge Blanket：膨張粒状スラッジブランケット式）のメタン発酵処理が多く採用されている（特許文献１参照）。グラニュールを利用した処理の場合、処理槽内に嫌気性微生物を保持できるため、高負荷で廃水を処理することができる。   In the treatment of organic wastewater such as wastewater from factories, etc., UASB method (Upflow Anaerobic Sludge Blanket) that uses granules (eg, granule methane) among anaerobic treatments Alternatively, many methane fermentation treatments of EGAB type (Expanded Granular Sludge Blanket type) are employed (see Patent Document 1). In the case of treatment using granules, anaerobic microorganisms can be retained in the treatment tank, so that wastewater can be treated with a high load.

しかしながら、有機性廃水中に硫酸イオンや亜硫酸イオンが含まれていると、嫌気性処理槽において硫化水素（Ｈ２Ｓ）等の硫化物が発生し、これがメタン発酵を阻害する。 However, when organic wastewater contains sulfate ions or sulfite ions, sulfides such as hydrogen sulfide (H 2 S) are generated in the anaerobic treatment tank, which inhibits methane fermentation.

このため、従来においては、嫌気性処理槽の前段に、有機性廃水から硫酸イオン及び亜硫酸イオンを除去するための手段を設けている。すなわち、亜硫酸イオンに対して、曝気により亜硫酸イオンを大気中に放散するための曝気槽を設けている。また、硫酸イオンに対しては、バリウム等の無機剤と反応させて硫酸バリウムとするための反応槽と、得られた硫酸バリウムを沈降分離させる沈殿槽とを設けているのである。
特開２００１−９４９４号公報 For this reason, conventionally, a means for removing sulfate ions and sulfite ions from the organic wastewater is provided in the front stage of the anaerobic treatment tank. In other words, an aeration tank is provided for sulfite ions to diffuse the sulfite ions into the atmosphere by aeration. For sulfate ions, a reaction vessel for reacting with an inorganic agent such as barium to form barium sulfate and a precipitation vessel for settling and separating the obtained barium sulfate are provided.
JP 2001-9494 A

しかしながら、上述したような硫酸イオン及び亜硫酸イオンの除去手段は、比較的大きな曝気槽と沈殿槽、そして反応槽も必要であり、廃水処理装置全体の大型化を招くという問題点がある。   However, the above-described means for removing sulfate ions and sulfite ions requires a relatively large aeration tank, precipitation tank, and reaction tank, and there is a problem in that the whole waste water treatment apparatus is increased in size.

そこで、本発明の主目的は、比較的小型の廃水処理装置であっても硫酸イオンや亜硫酸イオンを含有する有機性廃水を高度に処理することのできる処理方法を提供することにある。   Therefore, a main object of the present invention is to provide a treatment method capable of highly treating organic wastewater containing sulfate ions and sulfite ions even with a relatively small wastewater treatment apparatus.

上記目的を達成するために、本発明による有機性廃水の処理方法は、硫酸イオン及び／又は亜硫酸イオンを含有する有機性廃水を酸生成処理すると共に、硫酸イオン及び／又は亜硫酸イオンを還元して硫化物を生成する第１ステップと、第１ステップにより得られた硫化物を含む有機性廃水に鉄塩系の無機凝集剤を添加して硫化物を凝集し当該有機性廃水から分離する第２ステップと、第２ステップにより得られた硫化物が分離された有機性廃水を嫌気性処理する第３ステップとを含むことを特徴としている。   In order to achieve the above object, a method for treating organic wastewater according to the present invention comprises treating an organic wastewater containing sulfate ions and / or sulfite ions with acid, and reducing sulfate ions and / or sulfite ions. A first step of generating sulfide, and a second step of adding an iron salt-based inorganic flocculant to the organic wastewater containing sulfide obtained in the first step to aggregate the sulfide and separate it from the organic wastewater. And a third step of anaerobically treating the organic waste water from which the sulfide obtained in the second step is separated.

この方法では、嫌気性処理を行う前に硫酸イオン及び亜硫酸イオンが有機性廃水から除去されるため、嫌気性処理では廃水中の有機性成分のメタン発酵が円滑に行われる。   In this method, since sulfate ions and sulfite ions are removed from the organic wastewater before the anaerobic treatment, methane fermentation of organic components in the wastewater is smoothly performed in the anaerobic treatment.

第２ステップで得られた分離物を酸処理した場合、再溶解される。その処理液には、先に添加された無機凝集剤が含まれているため、これを第２ステップで用いる無機凝集剤として再利用することが有効である。   When the isolate obtained in the second step is acid-treated, it is redissolved. Since the treatment liquid contains the inorganic flocculant previously added, it is effective to reuse it as the inorganic flocculant used in the second step.

また、本発明は、上記方法を実施するに適した処理装置にも関する。当該処理装置は、有機性固形物を含有する有機性廃水に含まれている有機性成分を酸発酵反応させる酸生成槽と、この酸生成槽で処理された処理液を凝集剤の添加により固液分離処理する凝集沈殿槽と、凝集沈殿槽で分離された処理液を嫌気性処理する嫌気性処理槽とを備えることを特徴としている。   The present invention also relates to a processing apparatus suitable for carrying out the above method. The said processing apparatus solidifies the acid generation tank which carries out the acid-fermentation reaction of the organic component contained in the organic waste water containing an organic solid substance, and the processing liquid processed in this acid generation tank by addition of a flocculant. A coagulation sedimentation tank for liquid separation treatment and an anaerobic treatment tank for anaerobic treatment of the treatment liquid separated in the coagulation sedimentation tank are provided.

この構成では、上記方法を容易に実施できる他、有機性廃水に含まれている懸濁物質のような微細な有機性固形物を凝集沈殿槽で取り除くことができるため、後段での嫌気性処理槽に廃水に有機性固形物が随伴されることはなく、この点でも嫌気性処理槽での有機性成分の処理が高効率で行われることになる。   In this configuration, the above method can be easily implemented, and fine organic solids such as suspended solids contained in organic wastewater can be removed in the coagulation sedimentation tank, so anaerobic treatment at the later stage The tank is not accompanied by organic solids in the wastewater, and in this respect as well, the processing of organic components in the anaerobic treatment tank is performed with high efficiency.

また、本発明による処理装置は、凝集沈殿槽で分離された固体分を酸処理する酸処理槽を更に備え、酸処理槽で処理された処理液を酸生成槽又は凝集沈殿槽、或いは、その両方に返送するようになっていることを特徴としている。これにより、発生汚泥量が大幅に減じられる。また、酸処理槽からの処理液には凝集剤が含まれるため、これを再利用することができる。   Moreover, the treatment apparatus according to the present invention further includes an acid treatment tank for acid-treating the solid content separated in the coagulation sedimentation tank, and the treatment liquid treated in the acid treatment tank is converted into an acid generation tank or a coagulation sedimentation tank, or its It is characterized by being sent back to both. Thereby, the amount of generated sludge is greatly reduced. Further, since the treatment liquid from the acid treatment tank contains a flocculant, it can be reused.

なお、嫌気性処理槽としては上向流式嫌気性汚泥床槽であることが好適である。   The anaerobic treatment tank is preferably an upward flow type anaerobic sludge bed tank.

本発明の処理方法によれば、硫酸イオンや亜硫酸イオンを含む有機性廃水であっても、高効率で嫌気性処理を行うことが可能となり、廃水規制されるＣＯＤ物質等を効果的に削減することができる。また、着色された有機性廃水は放流水の着色問題を引き起こすおそれがあるが、凝集沈殿処理を行うため、着色物質も除去されるという効果も同時に得られる。よって、本発明による処理装置からの処理水を、直接、河川放流することも可能となる。   According to the treatment method of the present invention, even an organic wastewater containing sulfate ions and sulfite ions can be subjected to anaerobic treatment with high efficiency, effectively reducing COD substances and the like that are regulated by wastewater. be able to. Moreover, although the colored organic waste water may cause a coloring problem of the discharged water, the effect of removing the colored substance is also obtained at the same time because the coagulation sedimentation treatment is performed. Therefore, the treated water from the treatment apparatus according to the present invention can be directly discharged into the river.

また、本発明によれば、有機性成分の酸生成処理又は酸発酵反応処理を用いて硫酸イオンや亜硫酸イオンを還元して硫化物とし、その後、この硫化物を鉄塩系無機凝集剤により凝集沈殿させることで除去するが、そのための設備は小型の酸生成槽と凝集沈殿槽で足りる。この酸生成及び凝集沈殿は有機性成分を除去するためのものでもあるので、廃水処理装置全体の小型化、効率化を図ることができる。   Further, according to the present invention, sulfate ions and sulfite ions are reduced to sulfide by using an acid generation treatment or acid fermentation reaction treatment of organic components, and then the sulfide is aggregated with an iron salt-based inorganic flocculant. It is removed by precipitation, but a small acid generation tank and a coagulation sedimentation tank are sufficient for that purpose. Since this acid generation and coagulation precipitation are also for removing organic components, it is possible to reduce the size and efficiency of the entire wastewater treatment apparatus.

本発明による処理装置は、本発明の処理方法の実施に適していることはもとより、嫌気性処理槽に至る前に有機性固形物を凝集沈殿することができるので、有機性固形物を多く包含する廃水にも適している。   The treatment apparatus according to the present invention not only is suitable for carrying out the treatment method of the present invention, but can coagulate and precipitate organic solids before reaching the anaerobic treatment tank, and therefore includes a large amount of organic solids. Suitable for wastewater.

以下、図面を参照して本発明の好適な実施形態について詳細に説明する。   DESCRIPTION OF EMBODIMENTS Hereinafter, preferred embodiments of the present invention will be described in detail with reference to the drawings.

図１は、本発明による有機性廃水の処理方法に適した処理装置の一実施形態を示す概略説明図である。なお、本実施形態に係る処理装置が処理する廃水は、有機性固形物を多く含有し且つ硫酸イオン及び亜硫酸イオンを含有する廃水であるものとする。   FIG. 1 is a schematic explanatory view showing an embodiment of a treatment apparatus suitable for the organic wastewater treatment method according to the present invention. In addition, the wastewater which the processing apparatus which concerns on this embodiment processes shall be a wastewater which contains many organic solid substances and contains a sulfate ion and a sulfite ion.

図１に示すように、本実施形態に係る処理装置１０は、酸生成槽１２、凝集沈殿槽１４及び嫌気性処理槽１６を備えている。   As shown in FIG. 1, the treatment apparatus 10 according to this embodiment includes an acid generation tank 12, a coagulation sedimentation tank 14, and an anaerobic treatment tank 16.

酸生成槽１２には、廃水がライン１８を通して直接、或いは、廃水中に大きな夾雑物が含まれる場合にはそれを除去するための適当なフィルタ（図示せず）を介して、導入されるようになっている。この酸生成槽１２では、酸発酵反応を行う通性嫌気性微生物を液相内に浮遊状態で保持しており、廃水中の有機性成分を有機酸（低級脂肪酸）等に分解することが可能となっている。また、この酸発酵反応に伴って、廃水中の硫酸イオン及び亜硫酸イオンは還元され、硫化水素等の硫化物に変換される。この硫化物は溶存状態となっており、ライン２０を通して廃水と共に凝集沈殿槽１４に輸送される。この段階で、廃水中の液相には硫酸イオンと亜硫酸イオンは殆ど取り除かれた状態となる。   In the acid generator 12, the waste water is introduced directly through the line 18 or through a suitable filter (not shown) for removing large contaminants if the waste water contains large contaminants. It has become. In this acid generation tank 12, facultative anaerobic microorganisms that carry out an acid fermentation reaction are held in a suspended state in the liquid phase, and it is possible to decompose organic components in wastewater into organic acids (lower fatty acids) and the like. It has become. In addition, accompanying this acid fermentation reaction, sulfate ions and sulfite ions in the wastewater are reduced and converted to sulfides such as hydrogen sulfide. This sulfide is in a dissolved state and is transported to the coagulating sedimentation tank 14 along with the waste water through the line 20. At this stage, the liquid phase in the wastewater is almost free of sulfate ions and sulfite ions.

凝集沈殿槽１４は、例えば特開2001-286704号公報等に開示されたものが知られており、被処理液である有機性廃水に含まれている懸濁物質等を適当な凝集剤により凝集しフロック化すると共に、かかる廃水を槽内に均等配分して被処理液から懸濁物質等の固形物を沈殿除去しようとする沈降分離方式の固液分離装置の一種である。   The coagulation sedimentation tank 14 is known, for example, as disclosed in Japanese Patent Application Laid-Open No. 2001-286704 and the like, and suspended substances contained in organic waste water that is a liquid to be treated are coagulated with an appropriate coagulant. It is a kind of sedimentation-type solid-liquid separation device that flocates and disperses the waste water evenly in the tank and precipitates and removes solids such as suspended substances from the liquid to be treated.

酸生成槽１２から凝集沈殿槽１４へのライン２０には、廃水中の硫化物及び有機性懸濁物質を凝集するために、鉄塩系の無機凝集剤が導入されるようになっている。鉄塩系の無機凝集剤としては、硫酸鉄、ポリ硫酸鉄、塩化鉄等があげられる。また、この凝集を円滑に行わせるために、必要に応じて、適宜、アルカリ等の中和剤や高分子凝集剤が添加される。   An iron salt-based inorganic flocculant is introduced into the line 20 from the acid generation tank 12 to the coagulation sedimentation tank 14 in order to coagulate sulfides and organic suspended substances in the wastewater. Examples of iron salt-based inorganic flocculants include iron sulfate, polyiron sulfate, and iron chloride. Moreover, in order to perform this aggregation smoothly, neutralizers, such as an alkali, and a polymer flocculant are added suitably as needed.

凝集沈殿槽１４において、鉄塩系無機凝集剤や高分子凝集剤が添加された有機性廃水中の硫化物や有機性の懸濁物質等が凝集しフロック化する。そして、このフロック化した固形物を含有する廃水が凝集沈殿槽１４内に均等に配分されると、その後、下方には固体分、上方には固体分が除去された液体分に分離される。固体分には硫化物の大部分が含まれているため、液体分、特に上澄み液には硫黄分は含まれていないものとなる。凝集沈殿槽１４の底部からは固体分が汚泥として取り出される。この汚泥については後述する。   In the coagulation sedimentation tank 14, sulfides, organic suspended substances, etc. in the organic waste water to which the iron salt inorganic coagulant and the polymer coagulant are added aggregate and flock. Then, when the waste water containing the flocked solid matter is evenly distributed in the coagulation sedimentation tank 14, it is separated into a solid component in the lower portion and a liquid component from which the solid component is removed in the upper portion. Since the solid content contains most of the sulfide, the liquid content, particularly the supernatant, does not contain sulfur. From the bottom of the coagulation sedimentation tank 14, the solid is taken out as sludge. This sludge will be described later.

凝集沈殿槽１４での固液分離は薬剤を使用しているため、通常の沈殿槽に比して高速で行われ、また小型の槽であっても十分な処理結果が得られる。そして、凝集沈殿槽１４内の上澄液は、固形物が概ね除去された比較的清浄な有機性廃水となっており、この有機性廃水はライン２２を通して嫌気性処理槽１６に供給される。   Since the solid-liquid separation in the coagulation sedimentation tank 14 uses chemicals, it is performed at a higher speed than a normal sedimentation tank, and sufficient processing results can be obtained even with a small tank. The supernatant liquid in the coagulation sedimentation tank 14 is a relatively clean organic waste water from which solids are substantially removed, and this organic waste water is supplied to the anaerobic treatment tank 16 through the line 22.

嫌気性処理槽１６は、嫌気性微生物により有機性成分をメタンガスや炭酸ガス等に分解するためのものであり、ＥＧＳＢ式やＵＡＳＢ式処理槽のような上向流式嫌気性汚泥床槽等、種々の型式のものを適用可能であるが、本実施形態ではＵＡＳＢ式処理槽が用いられている。   The anaerobic treatment tank 16 is for decomposing organic components into methane gas, carbon dioxide gas, etc. by anaerobic microorganisms, such as an upflow anaerobic sludge bed tank such as an EGSB type or UASB type treatment tank, Although various types can be applied, a UASB processing tank is used in this embodiment.

ＵＡＳＢ式処理槽１６は、メタン菌を自己固定化して形成された固定化菌体、いわゆるグラニュールメタン菌が槽の下部にてスラッジ層１６ａとして保持されたものである。このＵＡＳＢ式処理槽においては、グラニュールメタン菌のスラッジ層１６ａは処理水と共に流出することがなく、処理槽１６内に保持されるのでメタン菌濃度を高く維持できるという特徴を有している。そのため、高負荷で廃水を高速で処理することができるという利点がある。図示の処理槽１６内では、スラッジ層１６ａは、スラッジベッド層と、その上側に形成されるスラッジブランケット層とからなっているが、高負荷化のために流速を高くした場合には、層間の区別は殆どなくなり、主にスラッジブランケット層のみの形となる。図示実施形態において、凝集沈殿槽１４からのライン２２に接続されたノズル２４は、スラッジベッド層に配設されている。ノズル２４は、凝集沈殿槽１４からの有機性廃水を処理槽１６内に均一に供給できるよう構成されている。   The UASB type treatment tank 16 is an immobilized microbial cell formed by self-immobilizing methane bacteria, so-called granule methane bacteria, which are held as a sludge layer 16a at the bottom of the tank. In this UASB type treatment tank, the sludge layer 16a of granule methane bacteria does not flow out together with the treated water, and is retained in the treatment tank 16, so that the concentration of methane bacteria can be maintained high. Therefore, there is an advantage that waste water can be treated at high speed with high load. In the illustrated processing tank 16, the sludge layer 16a is composed of a sludge bed layer and a sludge blanket layer formed on the upper side. However, when the flow rate is increased to increase the load, the sludge layer 16a There is almost no distinction, mainly in the form of a sludge blanket layer. In the illustrated embodiment, a nozzle 24 connected to a line 22 from the coagulation sedimentation tank 14 is disposed in the sludge bed layer. The nozzle 24 is configured to uniformly supply the organic waste water from the coagulation sedimentation tank 14 into the treatment tank 16.

ＵＡＳＢ式処理槽１６において、凝集沈殿槽１４から送られてきた有機性廃水中の残存している有機性成分はスラッジ層１６ａにおいてグラニュールメタン菌の働きによりメタンガスや炭酸ガス等に分解される。この場合、凝集沈殿槽１４において既に有機性廃水中からは硫酸イオンや亜硫酸イオンが殆ど除去されているため、処理槽１６においてはメタン発酵を阻害する硫化物も生ぜず、円滑に嫌気性処理が進められる。このようにして、酸生成槽１２及び凝集沈殿槽１４では除去できなかった有機性成分も分解され、ほぼ完全に有機性廃水中から除去されることになる。   In the UASB type treatment tank 16, the remaining organic components in the organic wastewater sent from the coagulation sedimentation tank 14 are decomposed into methane gas, carbon dioxide gas, etc. by the action of granule methane bacteria in the sludge layer 16a. In this case, since most of the sulfate ions and sulfite ions have already been removed from the organic wastewater in the coagulation sedimentation tank 14, the treatment tank 16 does not generate sulfides that inhibit methane fermentation, and smoothly performs anaerobic treatment. It is advanced. In this way, organic components that could not be removed in the acid generation tank 12 and the coagulation sedimentation tank 14 are also decomposed and removed almost completely from the organic waste water.

分解処理により発生したガスはＵＡＳＢ式処理槽１６の上部のガス排出ライン２６から排出される。排出されるガスの主成分であるメタンガスは、燃料として再利用することが可能であるので、排出ガスを適当なガス分離装置（図示せず）に通し、メタンガスを回収することが有効である。   The gas generated by the decomposition process is discharged from the gas discharge line 26 at the upper part of the UASB type processing tank 16. Since methane gas, which is the main component of the exhausted gas, can be reused as fuel, it is effective to collect the methane gas by passing the exhaust gas through an appropriate gas separation device (not shown).

有機性廃水はＵＡＳＢ式処理槽１６で処理されると、前述したように有機性成分が固形物も含めてガス化され除去されるため、処理槽１６から排出される処理水の水質性状は、ＣＯＤ物質の少ない良好のものとなる。従って、ライン２８を通して直接系外に放流したり、更にオゾン処理や活性炭処理等を施して再利用したりすることができる。なお、処理水の一部は、ライン３０を通して酸生成槽１２に返送してもよい。これは、処理槽１６内で処理された処理水に未だ処理されなかった有機性成分が残存している場合には、これを酸生成槽１２にて再度処理する目的の他、処理水に残存している中和剤や通性嫌気性微生物等を酸生成槽１２で再利用するためである。   When the organic waste water is treated in the UASB type treatment tank 16, the organic components including the solids are gasified and removed as described above. Therefore, the water quality of the treated water discharged from the treatment tank 16 is as follows. Good with less COD material. Therefore, it can be directly discharged out of the system through the line 28, or can be reused after being subjected to ozone treatment or activated carbon treatment. A part of the treated water may be returned to the acid generation tank 12 through the line 30. This is because, in the treated water treated in the treatment tank 16, when an organic component that has not yet been treated remains, it remains in the treated water in addition to the purpose of treating it again in the acid generation tank 12. This is because the neutralizing agent, facultative anaerobic microorganisms and the like are reused in the acid generation tank 12.

更に、本実施形態に係る処理装置１０は、凝集沈殿槽１４の底部から取り出された汚泥を酸剤により再溶解処理するための酸処理槽３２を備えている。前述したように、凝集沈殿槽１４で分離された、硫化物及び有機性固形物を主として含む固体分は汚泥として凝集沈殿槽１４の底部から取り出され、ライン３４を経て酸処理槽３２に送られる。   Furthermore, the processing apparatus 10 according to this embodiment includes an acid treatment tank 32 for re-dissolving sludge taken out from the bottom of the coagulation sedimentation tank 14 with an acid agent. As described above, the solid content mainly containing sulfide and organic solids separated in the coagulation sedimentation tank 14 is taken out from the bottom of the coagulation sedimentation tank 14 as sludge, and sent to the acid treatment tank 32 via the line 34. .

酸処理槽３２では、酸剤、例えば塩酸が添加され、汚泥はこれにより再溶解される。酸処理に適した条件としては、ｐＨ１〜５、温度３０〜１００℃、より好ましくはｐＨ２〜３、温度４５〜９０℃である。また、反応時間は０．２〜２０時間、より好ましくは０．５〜５時間程度である。   In the acid treatment tank 32, an acid agent such as hydrochloric acid is added, and the sludge is redissolved thereby. The conditions suitable for the acid treatment are pH 1-5, temperature 30-100 ° C, more preferably pH 2-3, temperature 45-90 ° C. The reaction time is about 0.2 to 20 hours, more preferably about 0.5 to 5 hours.

酸処理槽３２から排出された処理液には、有機酸を生成するための通性嫌気性微生物や、凝集沈殿のために添加された無機凝集剤及び高分子凝集剤が含まれているため、これらを再利用するために、処理液はライン３６．３８，４０を通して酸生成槽１２及び／又は凝集沈殿槽１４に返送される。返送は直接行ってもよいが、処理液に金属等の固形物が含まれていることも多く、ライン３６中に固液分離装置４２を配置し、残存固形物を分離することが好ましい。固液分離装置４２としては、例えば、沈殿槽、凝集沈殿槽、浮上分離槽、ろ過分離槽、膜分離槽等が使用される。   Since the treatment liquid discharged from the acid treatment tank 32 contains a facultative anaerobic microorganism for generating an organic acid, an inorganic flocculant and a polymer flocculant added for agglomeration and precipitation, In order to recycle them, the processing liquid is returned to the acid generation tank 12 and / or the coagulation sedimentation tank 14 through the lines 36.38 and 40. Although the return may be performed directly, it is often the case that solids such as metals are contained in the processing liquid, and it is preferable to dispose the solid solid separation device 42 in the line 36 to separate the remaining solids. As the solid-liquid separation device 42, for example, a sedimentation tank, a coagulation sedimentation tank, a flotation separation tank, a filtration separation tank, a membrane separation tank, or the like is used.

以上述べたように、本実施形態では、酸生成槽で硫酸イオン及び亜硫酸イオンを還元して硫化物とし、その後、この硫化物を凝集沈殿により取り除くため、嫌気性処理は硫化物のない状態で行われる。従って。有機性成分の嫌気性処理が円滑に行われ、廃水規制されるＣＯＤ物質等を効果的に削減することができ、直接、河川放流も可能となる。また、嫌気性処理槽１６に至るまでに有機性固形物も除去されるため、微細な有機性固形物が嫌気性処理槽１６のスラッジ層１６ａ，１６ｂを通過して系外に排出される心配もない。更に、凝集沈殿槽１４から汚泥として排出された硫化物及び有機性固形物は酸処理されるため、発生汚泥量も削減でき、加えて、その処理液を凝集沈殿槽１４に戻すことで処理液に含まれている無機凝集剤の再利用が可能となる。更にまた、凝集沈殿槽１４よりも後段において、嫌気性処理槽１６を複数段、シリーズに接続した場合には、処理を阻害する有機性固形物が殆ど含まれていないため、処理能力を著しく向上させることも可能となる。   As described above, in the present embodiment, sulfate ions and sulfite ions are reduced to sulfides in the acid generation tank, and then the sulfides are removed by coagulation precipitation. Therefore, the anaerobic treatment is performed without sulfides. Done. Therefore. Anaerobic treatment of organic components is performed smoothly, COD substances and the like that are regulated by wastewater can be effectively reduced, and direct river discharge is also possible. Further, since organic solids are also removed before reaching the anaerobic treatment tank 16, there is a concern that fine organic solids pass through the sludge layers 16 a and 16 b of the anaerobic treatment tank 16 and are discharged out of the system. Nor. Furthermore, since sulfides and organic solids discharged as sludge from the coagulation sedimentation tank 14 are acid-treated, the amount of generated sludge can be reduced, and in addition, the treatment liquid is returned to the coagulation sedimentation tank 14 to treat it. The inorganic flocculant contained in can be reused. Furthermore, when the anaerobic treatment tanks 16 are connected to a plurality of stages and series after the coagulation sedimentation tank 14, the organic solids that impede the treatment are hardly contained, so that the processing capacity is remarkably improved. It is also possible to make it.

以上、本発明の好適な実施形態について詳細に説明したが、本発明は上記実施形態に限定されないことは言うまでもない。   As mentioned above, although preferred embodiment of this invention was described in detail, it cannot be overemphasized that this invention is not limited to the said embodiment.

例えば、上記の処理装置１０は硫酸イオンや亜硫酸イオンを含む廃水を処理するものとして説明したが、処理装置１０自体は有機性固形物を多く含む有機性廃水に対して効果的なものであるので、硫酸イオンや亜硫酸イオンが少量或いは全く含まない有機性廃水にも適用可能であることは勿論である。その場合、処理装置１０において硫酸イオンや亜硫酸イオンを除去する必要がないため、凝集沈殿槽１４に導入する廃水に対して、鉄塩系の無機凝集剤のみならず、硫酸アルミニウム、塩化アルミニウム、ポリ塩化アルミニウム等のアルミニウム塩を使用することができる。アルカリ剤での可溶化に適した条件としては、ｐＨ９〜１４、温度２５〜９５℃、より好ましくはｐＨ１０〜１３、温度４０〜８０℃である。   For example, although the said processing apparatus 10 demonstrated as what processes the wastewater containing a sulfate ion and a sulfite ion, since the processing apparatus 10 itself is effective with respect to the organic wastewater containing many organic solid substances. Of course, the present invention can also be applied to organic wastewater containing little or no sulfate ions or sulfite ions. In this case, since it is not necessary to remove sulfate ions and sulfite ions in the treatment apparatus 10, not only iron salt-based inorganic flocculants but also aluminum sulfate, aluminum chloride, poly Aluminum salts such as aluminum chloride can be used. The conditions suitable for solubilization with an alkaline agent are pH 9 to 14, temperature 25 to 95 ° C, more preferably pH 10 to 13 and temperature 40 to 80 ° C.

次に、本発明の作用効果を確認するために行った実施例及び比較例について述べる。以下の実施例及び比較例では、有機性廃水として、懸濁物質が９００ｍｇ／ｌ、全化学的酸素要求量（Ｔ−ＣＯＤｃｒ）が４３００ｍｇ／ｌ、溶解性化学的酸素要求量（Ｆ−ＣＯＤｃｒ）が２９００ｍｇ／ｌであるビール製造工場からの有機性廃水を用いた。また、この廃水に、硫酸イオンを９６０ｍｇ／ｌを添加した。   Next, examples and comparative examples performed for confirming the effects of the present invention will be described. In the following examples and comparative examples, as organic waste water, suspended substance is 900 mg / l, total chemical oxygen demand (T-CODcr) is 4300 mg / l, soluble chemical oxygen demand (F-CODcr) Organic wastewater from a beer factory with a 2900 mg / l was used. In addition, 960 mg / l of sulfate ion was added to this waste water.

実施例では、図１に示す構成と同様な処理装置を用意した。処理装置における酸生成槽は、その有効容積が１ｍ３のもの、凝集沈殿槽は、その有効容積が３ｍ３、表面積負荷が１ｍ／ｈのもの、嫌気性処理槽はＵＡＳＢ式で、その有効容積が３．５ｍ３のものを使用した。そして、有機性廃水を処理装置（酸生成槽）に１．０４ｍ３／ｈの速度で供給すると共に、嫌気性処理槽で処理された処理水の一部を酸生成槽に返送した。また、酸生成槽内はｐＨ７に調整し、酸生成槽から嫌気性処理槽に有機性廃水を１．２５ｍ３／ｈで供給し、嫌気性処理槽内は３８℃とした。 In the example, a processing apparatus having the same configuration as that shown in FIG. 1 was prepared. The acid generation tank in the treatment apparatus has an effective volume of 1 m 3 , the coagulation sedimentation tank has an effective volume of 3 m 3 and a surface area load of 1 m / h, and the anaerobic treatment tank is a UASB type, and its effective volume Of 3.5 m 3 was used. And while supplying organic wastewater to the processing apparatus (acid production | generation tank) at the speed | rate of 1.04 m < 3 > / h, a part of treated water processed with the anaerobic treatment tank was returned to the acid production | generation tank. The acid generation tank was adjusted to pH 7, organic waste water was supplied from the acid generation tank to the anaerobic treatment tank at 1.25 m 3 / h, and the inside of the anaerobic treatment tank was set to 38 ° C.

また、凝集沈殿槽の前で無機凝集剤として塩化鉄を、運転当初は添加量、第二鉄イオンとしてとして５００ｍｇ／ｌ、装置が安定した後は５０ｍｇ／ｌで添加すると共に、中和用の水酸化ナトリウムを添加し、次いで高分子凝集剤を１ｐｐｍ添加した。凝集沈殿槽で分離された汚泥は酸処理槽でｐＨ２、槽内温度７０℃、処理時間１０時間という条件で処理した後、処理物を固液分離装置としての自然沈降式沈殿槽へ供給した。その後、沈殿槽の上澄液を凝集沈殿槽に戻して、溶解している塩化鉄を無機凝集剤として再利用した。   In addition, iron chloride is added as an inorganic flocculant in front of the coagulating sedimentation tank. The addition amount is 500 mg / l as the ferric ion at the beginning of operation, and 50 mg / l after the apparatus is stabilized. Sodium hydroxide was added followed by 1 ppm of polymer flocculant. The sludge separated in the coagulation sedimentation tank was treated in the acid treatment tank under the conditions of pH 2, tank internal temperature 70 ° C., treatment time 10 hours, and then the treated product was supplied to a natural sedimentation precipitation tank as a solid-liquid separator. Thereafter, the supernatant of the precipitation tank was returned to the coagulation precipitation tank, and the dissolved iron chloride was reused as an inorganic flocculant.

以上の運転条件で処理を続けた結果、ＵＡＳＢ式嫌気性処理槽からの流出水の組成は、懸濁物質が３５ｍｇ／ｌ、Ｔ−ＣＯＤｃｒが２５０ｍｇ／ｌ、Ｆ−ＣＯＤｃｒが２００ｍｇ／ｌとなり、特に懸濁物質が大幅に除去されていることが分かった。また、発生汚泥量（系外に引き出された汚泥量）は１５ｋｇ／ｄａｙであった。また、処理装置の運転が定常になった後の無機凝集剤の添加量は運転初期の約１／１０の少ない量としているが、上記の通り、良好な処理水が得られた。   As a result of continuing the treatment under the above operating conditions, the composition of the effluent water from the UASB type anaerobic treatment tank was 35 mg / l of suspended solids, 250 mg / l of T-CODcr, 200 mg / l of F-CODcr, In particular, it was found that suspended substances were greatly removed. The amount of generated sludge (the amount of sludge drawn out of the system) was 15 kg / day. Moreover, although the addition amount of the inorganic flocculant after the operation | movement of a processing apparatus became steady, it was made into the small quantity of about 1/10 of the operation | movement initial stage, As mentioned above, favorable treated water was obtained.

また、比較例として、上記実施例の凝集沈殿槽に代えて、凝集剤を添加しない自然沈降式の沈殿槽（有効容積３ｍ３）を設置し、その他の条件は上記実施例との同条件で処理を行った。 As a comparative example, a natural sedimentation type sedimentation tank (effective volume 3 m 3 ) without adding a flocculant is installed instead of the aggregation sedimentation tank of the above example, and other conditions are the same as those of the above example. Processed.

その結果、硫化水素が生成され、この硫化水素が嫌気性処理槽でのメタン発酵を阻害して有機性廃水の処理が実質行われていないことが分かった。   As a result, it was found that hydrogen sulfide was generated, and this hydrogen sulfide hindered methane fermentation in the anaerobic treatment tank, so that organic waste water was not substantially treated.

本発明による有機性廃水の処理装置の好適な実施形態を示す概略説明図である。It is a schematic explanatory drawing which shows suitable embodiment of the processing apparatus of the organic wastewater by this invention.

符号の説明Explanation of symbols

１０…処理装置、１２…酸生成槽、１４…凝集沈殿槽、１６…嫌気性処理槽、３２…酸処理槽、４２…固液分離装置。   DESCRIPTION OF SYMBOLS 10 ... Treatment apparatus, 12 ... Acid production tank, 14 ... Coagulation sedimentation tank, 16 ... Anaerobic treatment tank, 32 ... Acid treatment tank, 42 ... Solid-liquid separation apparatus.

Claims (5)

硫酸イオン及び／又は亜硫酸イオンを含有する有機性廃水を酸生成処理すると共に、前記硫酸イオン及び／又は前記亜硫酸イオンを還元して硫化物を生成する第１ステップと、
前記第１ステップにより得られた硫化物を含む有機性廃水に鉄塩系の無機凝集剤を添加して硫化物を凝集し当該有機性廃水から分離する第２ステップと、
前記第２ステップにより得られた硫化物が分離された有機性廃水を嫌気性処理する第３ステップと、
を含む有機性廃水の処理方法。 A first step in which an organic wastewater containing sulfate ions and / or sulfite ions is subjected to an acid generation treatment, and the sulfate ions and / or the sulfite ions are reduced to generate sulfides;
A second step of adding an iron salt-based inorganic flocculant to the organic wastewater containing sulfide obtained in the first step to aggregate the sulfide and separate it from the organic wastewater;
A third step of anaerobically treating the organic wastewater from which the sulfide obtained in the second step has been separated;
For treating organic wastewater containing water. 前記第２ステップにより得られた分離物を酸処理し、その処理液を前記無機凝集剤として利用することを特徴とする請求項１に記載の有機性廃水の処理方法。   The method for treating organic wastewater according to claim 1, wherein the separated product obtained in the second step is subjected to an acid treatment, and the treatment liquid is used as the inorganic flocculant. 有機性固形物を含有する有機性廃水に含まれている有機性成分を酸発酵反応させる酸生成槽と、前記酸生成槽で処理された処理液を凝集剤の添加により固液分離処理する凝集沈殿槽と、前記凝集沈殿槽で分離された処理液を嫌気性処理する嫌気性処理槽とを備えることを特徴とする有機性廃水の処理装置。   An acid generation tank that causes an acid fermentation reaction of organic components contained in organic wastewater containing organic solids, and agglomeration in which a treatment liquid treated in the acid generation tank is subjected to solid-liquid separation treatment by adding a flocculant An organic wastewater treatment apparatus comprising: a sedimentation tank; and an anaerobic treatment tank for anaerobically treating the treatment liquid separated in the coagulation sedimentation tank. 前記凝集沈殿槽で分離された固体分を酸処理する酸処理槽を更に備え、前記酸処理槽で処理された処理液を前記酸生成槽及び／又は前記凝集沈殿槽に返送するようになっていることを特徴とする請求項１に記載の有機性廃水の処理装置。   It further comprises an acid treatment tank that acid-treats the solid content separated in the coagulation sedimentation tank, and the treatment liquid treated in the acid treatment tank is returned to the acid generation tank and / or the coagulation sedimentation tank. The apparatus for treating organic wastewater according to claim 1, wherein: 前記嫌気性処理槽が上向流式嫌気性汚泥床槽であることを特徴とする請求項３又は４に記載の有機性廃水の処理装置。   The apparatus for treating organic wastewater according to claim 3 or 4, wherein the anaerobic treatment tank is an upward flow type anaerobic sludge bed tank.
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KR100818675B1 (en) * 2007-04-24 2008-04-02 주식회사 이레환경테크 Method of purifying wastewater
JP2010194491A (en) * 2009-02-26 2010-09-09 Yanmar Co Ltd Wastewater treatment apparatus
KR101152210B1 (en) 2010-05-25 2012-07-11 권혁성 Organic Waste Disposal System with Improved Methane Yield and Method
JP2017029882A (en) * 2015-07-29 2017-02-09 株式会社クラレ Waste water treatment method using carrier
JP2017119242A (en) * 2015-12-28 2017-07-06 株式会社サピエナント Organic matter treatment system and organic matter treatment method
JP2018175529A (en) * 2017-04-17 2018-11-15 東急建設株式会社 Decomposition accelerator, and environmental cleanup method using the decomposition accelerator
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Cited By (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
KR100818675B1 (en) * 2007-04-24 2008-04-02 주식회사 이레환경테크 Method of purifying wastewater
JP2010194491A (en) * 2009-02-26 2010-09-09 Yanmar Co Ltd Wastewater treatment apparatus
KR101152210B1 (en) 2010-05-25 2012-07-11 권혁성 Organic Waste Disposal System with Improved Methane Yield and Method
JP2017029882A (en) * 2015-07-29 2017-02-09 株式会社クラレ Waste water treatment method using carrier
JP2017119242A (en) * 2015-12-28 2017-07-06 株式会社サピエナント Organic matter treatment system and organic matter treatment method
JP2018175529A (en) * 2017-04-17 2018-11-15 東急建設株式会社 Decomposition accelerator, and environmental cleanup method using the decomposition accelerator
JP7515166B2 (en) 2020-10-05 2024-07-12 株式会社エイブル Methane fermentation wastewater treatment equipment
CN114315045A (en) * 2021-12-13 2022-04-12 苏沃特环境(江苏)有限公司 Treatment system and treatment method for sulfate wastewater

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