JP2005238166A - Anaerobic ammonoxidation treatment method - Google Patents
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本発明は、アンモニア態窒素と亜硝酸態窒素を含有する原水を、アンモニア態窒素を電子供与体とし、亜硝酸態窒素を電子受容体とする独立栄養性脱窒微生物（以下「ＡＮＡＭＭＯＸ微生物」と称す場合がある。）を含むグラニュール汚泥を保持する反応槽に上向流で通液して嫌気的アンモニア酸化処理（以下「ＡＮＡＭＭＯＸ処理」と称す場合がある。）する方法において、沈降性の良いグラニュール汚泥を形成し、これを反応槽内に高濃度に保持することにより、安定かつ効率的な処理を行う方法に関する。 In the present invention, raw water containing ammonia nitrogen and nitrite nitrogen is used as an autotrophic denitrifying microorganism (hereinafter referred to as “ANAMOX microorganism”) having ammonia nitrogen as an electron donor and nitrite nitrogen as an electron acceptor. In a method of anaerobic ammonia oxidation treatment (hereinafter sometimes referred to as “ANAMMOX treatment”) by flowing upwardly into a reaction tank holding granule sludge containing The present invention relates to a method for performing stable and efficient treatment by forming good granular sludge and maintaining it in a reaction tank at a high concentration.
排水中に含まれるアンモニア態窒素は河川、湖沼及び海洋などにおける富栄養化の原因物質の一つであり、排液処理工程で効率的に除去する必要がある。一般に、排水中のアンモニア態窒素は、アンモニア態窒素をアンモニア酸化細菌により亜硝酸態窒素に酸化し、更にこの亜硝酸態窒素を亜硝酸酸化細菌により硝酸態窒素に酸化する硝化工程と、これらの亜硝酸態窒素及び硝酸態窒素を従属栄養性細菌である脱窒菌により、有機物を電子供与体として利用して窒素ガスにまで分解する脱窒工程との２段階の生物反応を経て窒素ガスにまで分解される。 Ammonia nitrogen contained in wastewater is one of the causative substances of eutrophication in rivers, lakes, and oceans, and it is necessary to remove it efficiently in the drainage treatment process. In general, ammonia nitrogen in wastewater is oxidized by ammonia oxidizing bacteria to nitrite nitrogen, and nitrifying nitrogen is oxidized to nitrate nitrogen by nitrite oxidizing bacteria. Nitrite nitrogen and nitrate nitrogen are subjected to denitrification bacteria, which are heterotrophic bacteria, and are converted into nitrogen gas through a two-stage biological reaction with a denitrification process in which organic matter is decomposed into nitrogen gas using an electron donor. Disassembled.
しかし、このような従来の硝化脱窒法では、脱窒工程において電子供与体としてメタノールなどの有機物を多量に必要とし、また硝化工程では多量の酸素が必要であるため、ランニングコストが高いという欠点がある。 However, such a conventional nitrification denitrification method requires a large amount of organic matter such as methanol as an electron donor in the denitrification step, and also requires a large amount of oxygen in the nitrification step, so that the running cost is high. is there.
これに対して、近年、アンモニア態窒素を電子供与体とし、亜硝酸態窒素を電子受容体とする独立栄養性微生物（自己栄養細菌）を利用し、アンモニア態窒素と亜硝酸態窒素とを反応させて脱窒する嫌気的アンモニア酸化処理（ＡＮＡＭＭＯＸ処理）法が提案された。この方法であれば、有機物の添加は不要であるため、従属栄養性の脱窒菌を利用する方法と比べて、コストを低減することができる。また、独立栄養性の微生物は収率が低く、汚泥の発生量が従属栄養性微生物と比較すると著しく少ないので、余剰汚泥の発生量を抑えることができる。更に、従来の硝化脱窒法で観察されるＮ２Ｏの発生がなく、環境に対する負荷を低減できるといった特長もある。 On the other hand, in recent years, ammonia nitrogen and nitrite nitrogen are reacted using autotrophic microorganisms (autotrophic bacteria) using ammonia nitrogen as an electron donor and nitrite nitrogen as an electron acceptor. An anaerobic ammonia oxidation treatment (ANAMOX treatment) method for denitrification by dehydration was proposed. If this method is used, it is not necessary to add an organic substance, so that the cost can be reduced as compared with a method using heterotrophic denitrifying bacteria. Moreover, since the yield of autotrophic microorganisms is low and the amount of sludge generated is significantly less than that of heterotrophic microorganisms, the amount of surplus sludge generated can be suppressed. Furthermore, there is also a feature that the generation of N 2 O observed by the conventional nitrification denitrification method does not occur and the burden on the environment can be reduced.
このＡＮＡＭＭＯＸ処理法はＡＮＡＭＭＯＸ微生物によって、アンモニア態窒素と約１．３倍量の亜硝酸態窒素とを、下記反応式（１）に従って、窒素ガスにする生物反応である。
ＮＨ４ ＋＋１．３２ＮＯ２ −＋０．０６６ＨＣＯ３ −＋０．１３Ｈ＋
→１．０２Ｎ２＋０．２６ＮＯ３ −＋０．０６６ＣＨ２Ｏ０．５Ｎ０．１５
＋２．０３Ｈ２Ｏ …（１）
This ANAMOX treatment method is a biological reaction in which ammonia nitrogen and about 1.3 times the amount of nitrite nitrogen are converted into nitrogen gas according to the following reaction formula (1) by an ANAMOX microorganism.
NH 4 + +1.32 NO 2 − +0.066 HCO 3 − + 0.13H +
→ 1.02N 2 + 0.26NO 3 − + 0.066CH 2 O 0.5 N 0.15
+ 2.03H 2 O (1)
従って、例えば、ＡＮＡＭＭＯＸ処理の前段において、排水中に含まれるアンモニア態窒素の一部分を亜硝酸態窒素に酸化し、ＡＮＡＭＭＯＸ処理において、これを原水として、残留するアンモニア態窒素と酸化により生成した亜硝酸態窒素とを反応させて除去することができる。 Therefore, for example, in the preceding stage of the ANAMOX treatment, a part of the ammonia nitrogen contained in the waste water is oxidized to nitrite nitrogen, and in the ANAMOX treatment, this is used as raw water to produce the remaining ammonia nitrogen and the nitrous acid generated by oxidation. It can be removed by reacting with nitrogen.
しかし、上記ＡＮＡＭＭＯＸ処理法では、反応に関与するＡＮＡＭＭＯＸ微生物がその収率が低い分、増殖速度が遅く、反応槽内に高濃度に保持することが困難であり、このために処理効率を高めることができないという問題があった。 However, in the above-mentioned ANAMMOX treatment method, the growth rate of the ANAMMOX microorganisms involved in the reaction is low and the growth rate is slow, and it is difficult to maintain a high concentration in the reaction tank. There was a problem that could not.
ところで、従属栄養性細菌である脱窒菌を利用する従来の硝化脱窒法では、原水を反応槽の下部より上向流で流入させ、菌の付着担体を用いることなく、汚泥をブロック化又は粒状化させて粒径１〜数ｍｍのグラニュール汚泥の汚泥床（スラッジブランケット）を形成させ、反応槽中に高濃度の微生物を保持して高負荷処理を行うＵＳＢ（Upflow Sludge Bed；上向流汚泥床）方式で処理が行われており、ＡＮＡＭＭＯＸ微生物についても、グラニュール汚泥を用いて、ＵＳＢ反応槽により高負荷で嫌気的アンモニア酸化処理を行うことが提唱されている（特開２００２−３４６５９３号公報）。
しかしながら、ＡＮＡＭＭＯＸ微生物のグラニュール汚泥を保持した反応槽に原水を上向流で通液して高負荷運転を継続すると、グラニュールが肥大して粒径が大きくなり、グラニュール内部に空洞が形成され、そこにガスが包括されることによって、グラニュールの沈降速度が著しく低下する。そして、その結果、グラニュールの浮上、更には槽内の上昇水流による反応槽からの流出が起こり、反応槽内にグラニュール汚泥を安定的に保持することが困難となるという問題がある。 However, when raw water is passed upwardly into the reaction tank holding the granulated sludge of ANMAMOX microorganisms and the high load operation is continued, the granules are enlarged and the particle size is increased, and a cavity is formed inside the granules. In addition, the inclusion of gas therein significantly reduces the sedimentation rate of the granules. As a result, there is a problem that the granule is floated, and the outflow from the reaction tank occurs due to the rising water flow in the tank, making it difficult to stably hold the granule sludge in the reaction tank.
本発明は上記の問題点を解決し、反応槽内にＡＮＡＭＭＯＸ微生物のグラニュール汚泥を保持して嫌気的アンモニア酸化処理を行うにあたり、沈降性のよいグラニュール汚泥を形成させて、反応槽内にグラニュール汚泥を高濃度に保持することによって、安定かつ効率的な処理を行う嫌気的アンモニア酸化処理方法を提供することを目的とする。 The present invention solves the above-mentioned problems, and in carrying out anaerobic ammonia oxidation treatment while holding the granule sludge of ANAMMOX microorganisms in the reaction tank, granule sludge with good sedimentation is formed in the reaction tank. An object of the present invention is to provide an anaerobic ammonia oxidation treatment method that performs stable and efficient treatment by maintaining granular sludge at a high concentration.
本発明の嫌気的アンモニア酸化処理方法は、アンモニア態窒素と亜硝酸態窒素を含有する原水を、アンモニア態窒素を電子供与体とし、亜硝酸態窒素を電子受容体とする独立栄養性脱窒微生物を含むグラニュール汚泥を保持する反応槽に上向流で通液して嫌気的アンモニア酸化処理する方法において、該反応槽に導入される水にカルシウム化合物を添加して該反応槽に通液することを特徴とする。 The anaerobic ammonia oxidation treatment method of the present invention is an autotrophic denitrifying microorganism using raw water containing ammonia nitrogen and nitrite nitrogen as an electron donor and ammonia nitrate as an electron acceptor. In a method of conducting an anaerobic ammonia oxidation treatment by flowing upward into a reaction tank holding granule sludge containing water, a calcium compound is added to water introduced into the reaction tank, and the liquid is passed through the reaction tank It is characterized by that.
ＡＮＡＭＭＯＸ微生物を含むグラニュールを保持したＵＳＢ反応槽の高負荷運転を継続すると、グラニュールの肥大化、グラニュール内部の空洞化が生じ、これによってグラニュールの沈降速度が著しく低下し、槽内の上昇水流により、グラニュールが反応槽から流出し易くなるが、ＵＳＢ反応槽に導入される水（以下「ＡＮＡＭＭＯＸ被処理水」と称す場合がある。）にカルシウム化合物を添加して、グラニュールにカルシウム成分を炭酸カルシウムやヒドロキシアパタイトの形にして取り込ませることによって、グラニュールの比重を高め、その沈降性を良好に維持させることができるようになる。 Continued high-load operation of a USB reaction tank holding granules containing ANAMMOX microorganisms causes granule enlargement and cavitation inside the granules, which significantly reduces the sedimentation rate of the granules. The rising water flow makes it easier for the granules to flow out of the reaction tank, but the calcium compound is added to the water introduced into the USB reaction tank (hereinafter sometimes referred to as “ANAMOX treated water”) to form the granules. By incorporating the calcium component in the form of calcium carbonate or hydroxyapatite, it is possible to increase the specific gravity of the granule and maintain its sedimentation well.
本発明において、カルシウム化合物は、ＵＳＢ反応槽の流入水のカルシウム濃度が２０ｍｇ／Ｌ以上となるように、或いは、ＵＳＢ反応槽の流入水の窒素成分に対するカルシウム成分の重量比（カルシウム／全窒素比。以下「Ｃａ／Ｔ−Ｎ比」と称す場合がある。）が０．０３以上となるように添加することが好ましい。 In the present invention, the calcium compound is used so that the calcium concentration of the inflow water of the USB reaction tank is 20 mg / L or more, or the weight ratio of the calcium component to the nitrogen component of the inflow water of the USB reaction tank (calcium / total nitrogen ratio). Hereinafter, it may be referred to as “Ca / TN ratio”.) Is preferably added so that 0.03 or more.
本発明において、ＵＳＢ反応槽に導入される水は、好ましくは窒素含有排水を亜硝酸型硝化して排水中のアンモニア態窒素の一部を亜硝酸態窒素に変換した硝化液であることが好ましいが、この場合、原水である窒素含有排水にカルシウム化合物が含まれていても、亜硝酸化工程におけるｐＨ調整のために炭酸ナトリウムや炭酸水素ナトリウムが添加されるため、これらのカルシウム成分は炭酸カルシウムとして固形化、析出してしまい、ＡＮＡＭＭＯＸグラニュールの内部に析出させることができない。そのため、亜硝酸化工程の後段で、ＵＳＢ反応槽に流入するＡＮＡＭＭＯＸ被処理水中にカルシウム化合物を添加することが重要である。 In the present invention, the water introduced into the USB reaction tank is preferably a nitrification liquid in which nitrogen-containing wastewater is nitrite-type nitrified to convert a part of ammonia nitrogen in the wastewater into nitrite nitrogen. However, in this case, even if the calcium compound is contained in the nitrogen-containing wastewater, which is the raw water, sodium carbonate and sodium hydrogen carbonate are added to adjust the pH in the nitritation process. As a result, it solidifies and precipitates and cannot be deposited inside the ANAMOX granule. For this reason, it is important to add a calcium compound to the ANAMOX treated water that flows into the USB reaction tank after the nitritation step.
本発明の嫌気的アンモニア酸化処理方法によれば、ＡＮＡＭＭＯＸ微生物を含むグラニュールを保持したＵＳＢ反応槽内に、沈降性の良いグラニュール汚泥を形成してその浮上、流出を防止し、グラニュール汚泥を反応槽内に高濃度に保持することにより、安定かつ効率的な嫌気的アンモニア酸化処理を行うことができる。 According to the anaerobic ammonia oxidation treatment method of the present invention, granule sludge having good sedimentation property is formed in a USB reaction tank holding granules containing ANAMOX microorganisms to prevent its floating and outflow. By maintaining a high concentration in the reaction tank, a stable and efficient anaerobic ammonia oxidation treatment can be performed.
以下に図面を参照して本発明の嫌気的アンモニア酸化処理方法の実施の形態を詳細に説明する。 Embodiments of the anaerobic ammonia oxidation treatment method of the present invention will be described below in detail with reference to the drawings.
図１は、本発明の嫌気的アンモニア酸化処理方法の実施に好適なＵＳＢ反応槽の一例を示す系統図である。 FIG. 1 is a system diagram showing an example of a USB reaction tank suitable for carrying out the anaerobic ammonia oxidation treatment method of the present invention.
このＵＳＢ反応槽１は、内部にＡＮＡＭＭＯＸ微生物のグラニュール汚泥床が形成され、底部にＡＮＡＭＭＯＸ被処理水の導入配管２が接続されている。反応槽１の上部には気液固分離装置３が設けられ、この気液固分離装置３から、処理水の排出配管４と処理水の一部を循環水として導入配管２に戻す循環配管５が引き出されている。また、導入配管２には、カルシウム化合物の注入配管６が接続されている。
The USB reaction tank 1 has a granulated sludge bed of ANAMOX microorganisms inside, and an introduction pipe 2 for the ANMOX treated water is connected to the bottom. A gas / liquid / solid separation device 3 is provided in the upper part of the reaction tank 1, and a
原水は、配管５からの循環水と共に配管２からＵＳＢ反応槽１の底部に導入される間に配管６よりカルシウム化合物が添加される。ＵＳＢ反応槽１に導入された原水は、ＡＮＡＭＭＯＸ微生物のグラニュール汚泥床を上向流で上昇する間に、ＡＮＡＭＭＯＸ微生物により嫌気的アンモニア酸化処理され、処理水が配管４より系外へ排出される。また、処理水の一部は配管５よりＡＮＡＭＭＯＸ被処理水の導入配管２に循環される。
While raw water is introduced into the bottom of the USB reaction tank 1 from the pipe 2 together with the circulating water from the
添加するカルシウム化合物としては、塩化カルシウム（ＣａＣｌ２）、水酸化カルシウム（Ｃａ（ＯＨ）２）等を用いることができ、カルシウム化合物は、ＡＮＡＭＭＯＸ被処理水の窒素濃度が比較的低く、１００〜６７０ｍｇ−Ｎ／Ｌである場合には、好ましくはＵＳＢ反応槽１の流入水中のカルシウム濃度が２０ｍｇ／Ｌ以上、特に２０〜１００ｍｇ／Ｌとなるように、また、ＡＮＡＭＭＯＸ被処理水の窒素濃度が比較的高く、６７０〜３０００ｍｇ−Ｎ／Ｌである場合には、ＵＳＢ反応槽１の流入水中のＣａ／Ｔ−Ｎ比が０．０３以上、特に０．０５〜０．２０となるように添加することが好ましい。カルシウム化合物添加量が上記範囲よりも少ないと、カルシウム化合物を添加したことによる本発明のグラニュール汚泥の沈降性向上効果を十分に得ることができず、多いとＡＮＡＭＭＯＸ反応によるｐＨ上昇に伴ない、反応槽出口や出口配管にスケールが生成してしまう。 As the calcium compound to be added, calcium chloride (CaCl 2 ), calcium hydroxide (Ca (OH) 2 ) or the like can be used, and the calcium compound has a relatively low nitrogen concentration in the ANMOX treated water, and is 100 to 670 mg. In the case of -N / L, the calcium concentration in the inflow water of the USB reaction tank 1 is preferably 20 mg / L or more, particularly 20 to 100 mg / L, and the nitrogen concentration of the ANMOX treated water is compared. When it is 670 to 3000 mg-N / L, it is added so that the Ca / TN ratio in the inflow water of the USB reaction tank 1 is 0.03 or more, particularly 0.05 to 0.20. It is preferable. If the calcium compound addition amount is less than the above range, the effect of improving the sedimentation property of the granule sludge of the present invention due to the addition of the calcium compound cannot be sufficiently obtained, and if it is more, the pH increases due to the ANAMOX reaction, Scales are generated at the reaction vessel outlet and outlet piping.
本発明の生物脱窒方法において、処理対象となるＡＮＡＭＭＯＸ被処理水は、アンモニア態窒素及び亜硝酸態窒素を含む水であり、有機物及び有機態窒素を含むものであってもよいが、これらは脱窒処理前に予めアンモニア態窒素になる程度まで分解しておくことが好ましく、また、溶存酸素濃度が高い場合には、必要に応じて溶存酸素を除去しておくことが好ましい。ＡＮＡＭＭＯＸ被処理水は無機物を含んでいてもよい。また、ＡＮＡＭＭＯＸ被処理水はアンモニア態窒素を含む液と亜硝酸態窒素を含む液を混合したものであってもよい。例えば、アンモニア態窒素を含む排水をアンモニア酸化微生物の存在下に好気性処理を行い、アンモニア態窒素の一部、好ましくはその１／２を亜硝酸に部分酸化したものをＡＮＡＭＭＯＸ被処理水とすることができる。更には、アンモニア態窒素を含む排水の一部をアンモニア酸化微生物の存在下に好気性処理を行い、アンモニア態窒素を亜硝酸に酸化し、アンモニア態窒素を含む排水の残部と混合したものをＡＮＡＭＭＯＸ被処理水としても良い。 In the biological denitrification method of the present invention, the ANAMOX treated water to be treated is water containing ammonia nitrogen and nitrite nitrogen, and may contain organic matter and organic nitrogen. It is preferable to decompose to ammonia nitrogen in advance before the denitrification treatment, and when the dissolved oxygen concentration is high, it is preferable to remove the dissolved oxygen as necessary. The ANAMOX treated water may contain an inorganic substance. Moreover, the ANAMOX treated water may be a mixture of a liquid containing ammonia nitrogen and a liquid containing nitrite nitrogen. For example, wastewater containing ammonia nitrogen is subjected to aerobic treatment in the presence of ammonia oxidizing microorganisms, and a portion of ammonia nitrogen, preferably one half of which is partially oxidized to nitrous acid, is treated as ANAMMOX treated water. be able to. Furthermore, a part of the waste water containing ammonia nitrogen is subjected to aerobic treatment in the presence of ammonia oxidizing microorganisms, the ammonia nitrogen is oxidized to nitrous acid, and the mixture of the remaining waste water containing ammonia nitrogen is mixed with ANAMMOX. It may be treated water.
一般的には、下水、し尿、嫌気性硝化脱離液等のアンモニア態窒素、有機態窒素及び有機物を含む排水が処理対象となる場合が多いが、この場合、これらを好気性又は嫌気性処理して有機物を分解し、有機態窒素をアンモニア態窒素に分解し、さらに部分亜硝酸化或いは、一部についての亜硝酸化を行った硝化液をＡＮＡＭＭＯＸ被処理水とすることが好ましい。 In general, wastewater containing ammonia nitrogen, organic nitrogen and organic matter such as sewage, human waste, anaerobic nitrification and desorption liquid is often treated. In this case, these are treated aerobically or anaerobically. Thus, it is preferable to use the nitrification liquid obtained by decomposing the organic matter, decomposing the organic nitrogen into ammonia nitrogen, and further performing partial nitritation or partial nitritation to be treated with ANAMOX.
ＡＮＡＭＭＯＸ被処理水のアンモニア態窒素と亜硝酸態窒素の割合はモル比でアンモニア態窒素１に対して亜硝酸態窒素０．５〜２、特に１〜１．５とするのが好ましい。ＡＮＡＭＭＯＸ被処理水中のアンモニア態窒素及び亜硝酸態窒素の濃度はそれぞれ５〜３０００ｍｇ／Ｌ、５〜２００ｍｇ／Ｌであることが好ましいが、処理水を循環して希釈すればこの限りではない。 The ratio of the ammonia nitrogen and nitrite nitrogen in the ANAMOX treated water is preferably 0.5 to 2, particularly 1 to 1.5, in terms of molar ratio with respect to ammonia nitrogen 1. The concentrations of ammonia nitrogen and nitrite nitrogen in the ANAMOX treated water are preferably 5 to 3000 mg / L and 5 to 200 mg / L, respectively, but the concentration is not limited as long as the treated water is circulated and diluted.
ＡＮＡＭＭＯＸ処理条件としては、例えば反応槽内液の温度が１０〜４０℃、特に２０〜３５℃、ｐＨが５〜９、特に６〜８、溶存酸素濃度が０〜２．５ｍｇ／Ｌ、特に０〜０．２ｍｇ／Ｌ、ＢＯＤ濃度が０〜５０ｍｇ／Ｌ、特に０〜２０ｍｇ／Ｌ、窒素負荷が０．１〜１０ｋｇ−Ｎ／ｍ３・ｄａｙ、特に１〜５ｋｇ−Ｎ／ｍ３・ｄａｙの範囲とするのが好ましい。 As the conditions for the ANAMOX treatment, for example, the temperature of the liquid in the reaction vessel is 10 to 40 ° C., particularly 20 to 35 ° C., the pH is 5 to 9, particularly 6 to 8, and the dissolved oxygen concentration is 0 to 2.5 mg / L, particularly 0. -0.2 mg / L, BOD concentration is 0-50 mg / L, especially 0-20 mg / L, nitrogen load is 0.1-10 kg-N / m 3 · day, especially 1-5 kg-N / m 3 · day It is preferable to be in the range.
グラニュール汚泥を形成する場合、微生物だけではグラニュール形成に期間を要するので、核となる物質を添加し、その核の周りにＡＮＡＭＭＯＸ微生物の生物膜を形成させても良い。この場合、核として、例えば微生物グラニュールや非生物的な担体を挙げることができる。 When granule sludge is formed, it takes a period of time for granule formation only with microorganisms. Therefore, a substance serving as a nucleus may be added to form a biofilm of ANAMOX microorganisms around the nucleus. In this case, examples of the nucleus include microbial granules and abiotic carriers.
核として用いられる微生物グラニュールとしては、メタン菌グラニュール等の嫌気性微生物や従属栄養性脱窒菌グラニュール等を挙げることができる。メタン菌グラニュールは、ＵＡＳＢ（Upflow Anaerobic Sludge Blanket；上向流嫌気性汚泥床）法もしくはＥＧＳＢ（Expanded Granule Sludge Bed；展開粒状汚泥床）法でメタン発酵が行われているメタン発酵槽で使用されているものを適用できる。また、従属栄養性脱窒グラニュールは、ＵＳＢ方式の通常の脱窒槽で利用されるものを適用できる。これらのグラニュールはそのままの状態で、又はその破砕物として用いることができる。ＡＮＡＭＭＯＸ微生物はこのような微生物グラニュールに付着しやすく、グラニュールの形成に要する時間が短縮される。また、核として非生物的な材料を用いるよりも経済的である。 Examples of the microorganism granules used as the nucleus include anaerobic microorganisms such as methane bacteria granules and heterotrophic denitrifying bacteria granules. Methane granule is used in methane fermentation tanks where methane fermentation is performed by UASB (Upflow Anaerobic Sludge Blanket) method or EGSB (Expanded Granule Sludge Bed) method You can apply what you have. The heterotrophic denitrification granules can be those used in a normal USB denitrification tank. These granules can be used as they are or as crushed materials thereof. ANAMMOX microorganisms are likely to adhere to such microbial granules, and the time required for the formation of granules is shortened. It is also more economical than using abiotic materials as the core.
核として用いられる非生物的な材料としては、例えば、活性炭、ゼオライト、ケイ砂、ケイソウ土、焼成セラミック、イオン交換樹脂等、好ましくは活性炭、ゼオライト等よりなる、粒径５０〜２００μｍ、好ましくは５０〜１００μｍで、平均比重１．０１〜２．５、好ましくは１．１〜２．０の担体を挙げることができる。 Examples of the abiotic material used as the core include activated carbon, zeolite, silica sand, diatomaceous earth, fired ceramic, ion exchange resin, and the like, preferably made of activated carbon, zeolite, and the like, and a particle size of 50 to 200 μm, preferably 50. A carrier having an average specific gravity of 1.01 to 2.5, preferably 1.1 to 2.0, can be mentioned.
このようにして形成されるＡＮＡＭＭＯＸ微生物のグラニュール汚泥は、平均粒径が０．２５〜３ｍｍ、好ましくは０．２５〜２ｍｍ、より好ましくは０．２５〜１．５ｍｍ程度、平均比重が１．０１〜２．５、好ましくは１．１〜２．０であることが望ましい。グラニュールの粒度が小さいほど比表面積が大きくなるので、高い汚泥濃度を維持し、嫌気的アンモニア酸化処理を効率よく行う点で好ましい。 The granulated sludge of the ANAMOX microorganism thus formed has an average particle size of 0.25 to 3 mm, preferably 0.25 to 2 mm, more preferably about 0.25 to 1.5 mm, and an average specific gravity of 1. It is desirable that it is 01 to 2.5, preferably 1.1 to 2.0. The smaller the granule particle size, the larger the specific surface area, which is preferable in that the high sludge concentration is maintained and the anaerobic ammonia oxidation treatment is efficiently performed.
本発明の嫌気的アンモニア酸化処理方法は、具体的には、嫌気性処理で見られるようなＵＡＳＢ方式又はＥＧＳＢ方式で反応槽内のＡＮＡＭＭＯＸ微生物のグラニュール汚泥を原水の上向流で展開させてグラニュール汚泥床を形成して行うのが、原水とグラニュール汚泥との接触効率を高くすることができ、好ましい。なお、処理水の一部は、必要に応じて循環水として、反応槽のＡＮＡＭＭＯＸ被処理水導入側へ戻す。 Specifically, the anaerobic ammonia oxidation treatment method of the present invention is a UASB method or an EGSB method as seen in anaerobic treatment, in which the granular sludge of ANAMOX microorganisms in the reaction tank is developed in the upstream flow of the raw water. It is preferable to form a granular sludge bed because the contact efficiency between the raw water and the granular sludge can be increased. In addition, a part of the treated water is returned to the ANAMOX treated water introduction side of the reaction tank as circulating water as necessary.
この場合、ＵＡＳＢ方式であれば循環水量はＡＮＡＭＭＯＸ被処理水量の０．５〜１０倍とし、反応槽内の上向流速（ＡＮＡＭＭＯＸ被処理水と循環水との合計の流速）を０．５〜４ｍ／ｈｒとするのが好ましい。また、ＥＧＳＢ方式であればＡＮＡＭＭＯＸ被処理水量は原水量の０．５〜２０倍とし、反応槽内の上向流速（ＡＮＡＭＭＯＸ被処理水と循環水の合計の流速）を２〜１５ｍ／ｈｒとしてグラニュール汚泥床を展開させて通液する。 In this case, in the case of the UASB method, the circulating water amount is 0.5 to 10 times the amount of the ANAMOX treated water, and the upward flow rate in the reaction tank (the total flow rate of the ANAMOX treated water and the circulating water) is 0.5 to It is preferably 4 m / hr. In the case of the EGSB method, the amount of water to be treated with ANAMMOX is 0.5 to 20 times the amount of raw water, and the upward flow rate in the reaction tank (the total flow rate of the water to be treated with ANAMMOX and circulating water) is 2 to 15 m / hr Expand the granular sludge bed and let it through.
本発明においては、ＡＮＡＭＭＯＸ微生物のグラニュール汚泥を保持する反応槽にＡＮＡＭＭＯＸ被処理水を上向流で通液して嫌気的アンモニア酸化処理するに当たり、反応槽にカルシウム化合物を添加しながら、ＡＮＡＭＭＯＸ被処理水を反応槽に通液するものであり、カルシウム化合物は、ＡＮＡＭＭＯＸ被処理水とは別の注入配管から注入することも可能であるが、ＡＮＡＭＭＯＸ被処理水と共に均一に反応槽に添加するために、図１に示す如く、ＡＮＡＭＭＯＸ被処理水の導入配管２にカルシウム化合物を注入することが好ましい。 In the present invention, when an AMAMOX treated water is passed in an upward flow through a reaction tank holding granulated sludge of ANAMOX microorganisms for anaerobic ammonia oxidation treatment, a calcium compound is added to the reaction tank, The treated water is passed through the reaction tank, and the calcium compound can be injected from an injection pipe different from the ANAMOX treated water, but is added to the reaction tank uniformly along with the ANAMOX treated water. In addition, as shown in FIG. 1, it is preferable to inject a calcium compound into the introduction pipe 2 of the ANAMOX treated water.
なお、図１のＵＳＢ反応槽１において、カルシウム化合物の注入配管は循環水の循環配管５に設けても良く、また、この循環配管５の接続位置よりも上流側の導入配管２に設けても良い。
In the USB reaction tank 1 of FIG. 1, the calcium compound injection pipe may be provided in the
以下に実施例を挙げて本発明をより具体的に説明する。 Hereinafter, the present invention will be described more specifically with reference to examples.
実施例１
図２に示す手順で、アンモニア態窒素濃度４５０〜６００ｍｇ−Ｎ／Ｌの原水の亜硝酸化処理を行った後、得られた硝化液（アンモニア態窒素濃度１５０〜３００ｍｇ−Ｎ／Ｌ，亜硝酸態窒素２００〜４００ｍｇ−Ｎ／Ｌ）にカルシウム化合物を添加して図１に示すＵＳＢ反応槽（容積２００Ｌ）でＡＮＡＭＭＯＸ処理を行った。ＵＳＢ反応槽では、流入水ｐＨ７．２〜７．５、温度３０〜３２℃、ＨＲＴ２ｈｒで、処理水に亜硝酸態窒素を２〜２０ｍｇ−Ｎ／Ｌ残存させる運転を行った。
Example 1
After performing nitritation treatment of raw water having an ammonia nitrogen concentration of 450 to 600 mg-N / L by the procedure shown in FIG. 2, the resulting nitrification solution (ammonia nitrogen concentration of 150 to 300 mg-N / L, nitrous acid) The calcium compound was added to 200-400 mg-N / L of nitrogen (N) and the ANAMOX treatment was performed in the USB reaction tank (volume 200 L) shown in FIG. In the USB reaction tank, the operation was performed such that 2 to 20 mg-N / L of nitrite nitrogen remained in the treated water at an influent water pH of 7.2 to 7.5, a temperature of 30 to 32 ° C., and an HRT of 2 hr.
この運転中にＵＳＢ反応槽内のグラニュール汚泥を１５〜３０日毎に採取して測定し、結果を図３に示した。 During this operation, granular sludge in the USB reaction tank was sampled and measured every 15-30 days, and the results are shown in FIG.
まず、ＵＳＢ反応槽に導入するＡＮＡＭＭＯＸ被処理水にカルシウム化合物として塩化カルシウムを添加してこの被処理水中のカルシウム濃度が１３〜１５ｍｇ／Ｌ（Ｃａ／Ｔ−Ｎが０．０２〜０．０３）として処理を行ったところ、この期間のＡＮＡＭＭＯＸグラニュール汚泥の沈降速度は運転開始時には３５ｍ／ｈｒであったが、次第に減少し、運転開始から２２０日目には２７ｍ／ｈｒまで低下する結果が得られた。 First, calcium chloride is added as a calcium compound to the ANAMOX treated water introduced into the USB reaction tank, and the calcium concentration in the treated water is 13 to 15 mg / L (Ca / TN is 0.02 to 0.03). As a result, the sedimentation rate of the ANAMOX granule sludge during this period was 35 m / hr at the start of operation, but gradually decreased, and the result decreased to 27 m / hr on the 220th day after the start of operation. It was.
続いて、運転開始から２６０日目（図３のＡ点）より、アンモニア態窒素濃度が３００〜５００ｍｇ−Ｎ／Ｌの原水を亜硝酸化処理し、得られた硝化液（アンモニア態窒素濃度１００〜３００ｍｇ−Ｎ／Ｌ，亜硝酸態窒素１５０〜３００ｍｇ−Ｎ／Ｌ）をＡＮＡＭＭＯＸ被処理水として上記と同様にしてＡＮＡＭＭＯＸ処理を行った。このときのＡＮＡＭＭＯＸ被処理水中のカルシウム濃度は３０〜４０ｍｇ−Ｎ／ＬでＣａ／Ｔ−Ｎは０．０６〜０．１３であった。その結果、この原水のアンモニア態窒素濃度変更から３０日後に、それまで減少していたグラニュール汚泥の沈降速度が上昇傾向に転じ、６０日後には運転開始時と同程度の３５ｍ／ｈｒにまで回復した。 Subsequently, from 260 days after starting operation (point A in FIG. 3), raw water having an ammonia nitrogen concentration of 300 to 500 mg-N / L was subjected to nitritation treatment, and the resulting nitrification solution (ammonia nitrogen concentration 100) ˜300 mg-N / L, nitrite nitrogen 150-300 mg-N / L) was used as the ANAMOX treated water and subjected to the ANAMOX treatment in the same manner as described above. The calcium concentration in the ANAMOX treated water at this time was 30 to 40 mg-N / L, and Ca / TN was 0.06 to 0.13. As a result, 30 days after the change of the ammonia nitrogen concentration of the raw water, the sedimentation rate of the granular sludge that had decreased until then began to increase, and after 60 days, it reached 35 m / hr, the same level as at the start of operation. Recovered.
このことから、ＡＮＡＭＭＯＸ被処理水のＣａ／Ｔ−Ｎが０．０３以上となるようにカルシウム化合物を添加することにより、グラニュール汚泥の沈降性を高めることができることが分かる。 This shows that the sedimentation property of granule sludge can be improved by adding a calcium compound so that Ca / T-N of ANAMOX treated water becomes 0.03 or more.
１ ＵＳＢ反応槽
３ 気液固分離装置
1 USB reaction tank 3 Gas-liquid solid separation device
Claims (4)
該反応槽に導入される水にカルシウム化合物を添加して該反応槽に通液することを特徴とする嫌気的アンモニア酸化処理方法。 The raw water containing ammonia nitrogen and nitrite nitrogen is put into a reaction tank holding granulated sludge containing autotrophic denitrifying microorganisms with ammonia nitrogen as an electron donor and nitrite nitrogen as an electron acceptor. In the method of anaerobic ammonia oxidation treatment by flowing in an upward flow,
An anaerobic ammonia oxidation method characterized by adding a calcium compound to water introduced into the reaction vessel and passing the solution through the reaction vessel.
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