JP2001079593A - Removing method of nitrogen in waste water - Google Patents
Removing method of nitrogen in waste waterInfo
- Publication number
- JP2001079593A JP2001079593A JP25968499A JP25968499A JP2001079593A JP 2001079593 A JP2001079593 A JP 2001079593A JP 25968499 A JP25968499 A JP 25968499A JP 25968499 A JP25968499 A JP 25968499A JP 2001079593 A JP2001079593 A JP 2001079593A
- Authority
- JP
- Japan
- Prior art keywords
- nitrogen
- bacteria
- wastewater
- tank
- sulfur
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Classifications
-
- Y02W10/12—
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、従属栄養細菌およ
び独立栄養細菌である硫黄酸化細菌と硝化細菌を用い
て、排水中に含まれる窒素化合物を効率的に除去する方
法に関する。TECHNICAL FIELD The present invention relates to a method for efficiently removing nitrogen compounds contained in wastewater by using heterotrophic bacteria and autotrophic bacteria, sulfur oxidizing bacteria and nitrifying bacteria.
【０００２】[0002]
【従来の技術】排水からの窒素の除去方法としては、生
物学的脱窒素方法が広く知られている。排水中の窒素の
形態としてはアンモニア性窒素の形で含有されることが
多い。特に高濃度のアンモニア性窒素を含有する排水
は、製鉄所コークス工場、屎尿、肥料工場、半導体工
場、皮革工場などから発生する。特に、製鉄所コークス
工場から発生するアンモニア性窒素含有排水は安水とも
呼ばれ、アンモニア性窒素を数百〜数千ｍｇ／ｌ程度も
含有している。2. Description of the Related Art As a method for removing nitrogen from wastewater, a biological denitrification method is widely known. The form of nitrogen in wastewater is often contained in the form of ammoniacal nitrogen. In particular, wastewater containing a high concentration of ammonia nitrogen is generated from a coke factory, a human waste, a fertilizer factory, a semiconductor factory, a leather factory, and the like. In particular, the wastewater containing ammonia nitrogen generated from a coke plant of an ironworks is also referred to as low water, and contains about several hundred to several thousand mg / l of ammonia nitrogen.
【０００３】排水からのアンモニア性窒素の生物学的除
去方法としては、好気性独立栄養細菌（ニトロゾモナ
ス、ニトロバクター等の硝化細菌）による生物学的酸化
と通性嫌気性従属栄養細菌（シュードモナス等）による
生物学的還元の組み合わせから成る生物学的硝化−脱窒
素法が広く知見されている。[0003] As a method for biologically removing ammonia nitrogen from wastewater, biological oxidation by aerobic autotrophic bacteria (nitrifying bacteria such as Nitrozomonas and Nitrobacter) and facultative anaerobic heterotrophic bacteria (Pseudomonas etc.) are known. The biological nitrification-denitrification process, which consists of a combination of biological reductions by A.
【０００４】まず、硝化工程は以下の２段の反応から成
っており、関与する硝化細菌の種類は異なっている。[0004] First, the nitrification process comprises the following two-stage reactions, and the types of nitrifying bacteria involved are different.
【０００５】 ２ＮＨ4 + ＋ ３Ｏ2 → ２ＮＯ2 -＋２Ｈ2Ｏ＋４Ｈ+ （１）[0005] 2NH 4 + + 3O 2 → 2NO 2 - + 2H 2 O + 4H + (1)
【０００６】 ２ＮＯ2 - ＋ Ｏ2 → ２ＮＯ3 - （２）2NO 2 − + O 2 → 2NO 3 − (2)
【０００７】（１）式に示す反応は、ニトロゾモナスを
代表種とする亜硝酸菌によってもたらされ、（２）式に
示す反応は、ニトロバクターを代表種とする硝酸菌によ
ってもたらされる。The reaction represented by the formula (1) is caused by nitrites represented by Nitrozomonas, and the reaction represented by the formula (2) is caused by nitrites represented by Nitrobacter.
【０００８】上記反応によって生成した亜硝酸性窒素な
らびに硝酸性窒素は、一般的に通性嫌気性従属栄養細菌
を用い、無酸素の条件下で以下のように還元されて酸化
窒素ガス（Ｎ2Ｏ）あるいは窒素ガス（Ｎ2）となり、大
気中に放散される。[0008] Nitrite nitrogen and nitrate nitrogen produced by the above reaction are reduced as follows under oxygen-free conditions using a facultative anaerobic heterotrophic bacterium, and nitric oxide gas (N 2 O) or nitrogen gas (N 2 ) and is released into the atmosphere.
【０００９】 ２ＮＯ2 - ＋ ６Ｈ2 → Ｎ2 ＋２Ｈ2Ｏ＋２ＯＨ- （３）2NO 2 − + 6H 2 → N 2 + 2H 2 O + 2OH − (3)
【００１０】 ２ＮＯ3 - ＋１０Ｈ2 → Ｎ2 ＋４Ｈ2Ｏ＋２ＯＨ- （４）2NO 3 − + 10H 2 → N 2 + 4H 2 O + 2OH − (4)
【００１１】通性嫌気性従属栄養細菌は水素供与体が必
要であり、有機物が通常利用される。都市下水などでは
下水中の有機物がそのまま用いられ、有機物を含まない
排水ではメタノールなどが添加されることが多い。A facultative anaerobic heterotrophic bacterium requires a hydrogen donor, and organic matter is usually used. In municipal sewage and the like, organic matter in sewage is used as it is, and in wastewater containing no organic matter, methanol or the like is often added.
【００１２】この生物学的硝化−脱窒素法は、アンモニ
ア性窒素濃度が１００ｍｇ／ｌ以下の排水では最も安価
で安定した処理方法で広く用いられている。This biological nitrification-denitrification method is widely used as the cheapest and stable treatment method for wastewater having an ammonia nitrogen concentration of 100 mg / l or less.
【００１３】[0013]
【発明が解決しようとする課題】しかし、生物学的硝化
−脱窒素法は、アンモニア性窒素濃度が１００ｍｇ／ｌ
を超えると様々な課題が生じ、安定した処理が困難とな
る。すなわち、アンモニア性窒素濃度が１００ｍｇ／ｌ
を超えると、硝化工程において、アンモニア性窒素の酸
化が硝酸性窒素まで進行しないこと、すなわち、ニトロ
バクターが阻害を受け、処理水中の亜硝酸性窒素が蓄積
しやすいことが知見されている。この原因として、遊離
のアンモニウムイオンのニトロバクターへの阻害が知ら
れている。特に、ｐＨが高いと遊離のアンモニウムイオ
ンが発生しやすい。However, the biological nitrification-denitrification method has an ammonia nitrogen concentration of 100 mg / l.
When the number exceeds, various problems occur, and stable processing becomes difficult. That is, the ammonia nitrogen concentration is 100 mg / l.
It has been found that, when the temperature exceeds the limit, in the nitrification step, the oxidation of ammoniacal nitrogen does not proceed to nitrate nitrogen, that is, the nitrobacter is inhibited, and the nitrite nitrogen in the treated water tends to accumulate. As a cause of this, inhibition of free ammonium ions on nitrobacter is known. In particular, when the pH is high, free ammonium ions are easily generated.
【００１４】亜硝酸性窒素は従属栄養細菌に対して毒性
が強く、処理水質が悪化しやすいことは広く知られてい
る（例えば、遠矢泰典、「下水道協会誌」、ＶＯＬ７、
ＮＯ７４、１９７０）。脱窒素に用いられている細菌
は、通常、従属栄養細菌であるから、蓄積した亜硝酸性
窒素によって脱窒素反応の進行に阻害が生ずる。脱窒素
反応の進行が停止すると、亜硝酸性窒素が処理水に流出
し、窒素規制をクリアできないばかりか、亜硝酸性窒素
起因のＣＯＤ（化学的酸素要求量）も増大してしまう。It is widely known that nitrite nitrogen is highly toxic to heterotrophic bacteria and easily deteriorates the quality of treated water (for example, Yasunori Toya, "Sewerage Association Journal", Vol.
NO 74, 1970). Since the bacteria used for denitrification are usually heterotrophic bacteria, the accumulated nitrite nitrogen inhibits the progress of the denitrification reaction. When the progress of the denitrification reaction is stopped, nitrite nitrogen flows out into the treated water, and not only nitrogen regulation cannot be cleared, but also COD (chemical oxygen demand) due to nitrite nitrogen increases.
【００１５】このようなことから、アンモニア性窒素濃
度が１００ｍｇ／ｌを超えるような排水の場合、従来の
生物学的硝化−脱窒素法の適用は、かなり難しい。[0015] For this reason, in the case of wastewater in which the concentration of ammonia nitrogen exceeds 100 mg / l, it is quite difficult to apply the conventional biological nitrification-denitrification method.
【００１６】例えば、「鉄と鋼」，ＶＯＬ８２，Ｎｏ．
５，４４７−４５２，１９９６には、生物学的硝化−脱
窒素法のコークス炉排水への適用事例が報告されてお
り、特に、亜硝酸性窒素濃度を５０ｍｇ／ｌ以下にしな
ければならないとされている。用いている脱窒素細菌
は、メタノールを添加していることから、従属栄養細菌
である。For example, “Iron and Steel”, VOL82, No.
No. 5,447-452, 1996 reports an application of a biological nitrification-denitrification method to coke oven effluent. In particular, it is required that the concentration of nitrite nitrogen be reduced to 50 mg / l or less. ing. The denitrifying bacteria used are heterotrophic bacteria because of the addition of methanol.
【００１７】ところで、脱窒性能を有する細菌は、従属
栄養細菌に限らない。水素細菌や硫黄酸化細菌などの独
立栄養細菌も、酸素の無い状態で脱窒素機能を有するこ
とは広く知られている。これらの独立栄養細菌は、それ
ぞれ水素や還元性硫黄化合物を酸化した時に発生するエ
ネルギーと空気中の炭酸ガスから菌体を合成し増殖す
る。これらの細菌は、増殖速度が小さいことやフロック
形成能力が弱いこと等の理由から、脱窒素作用が知られ
ているものの脱窒素に用いられた事例はほとんどない。Incidentally, the bacteria having the denitrifying performance are not limited to heterotrophic bacteria. It is widely known that autotrophic bacteria such as hydrogen bacteria and sulfur oxidizing bacteria also have a denitrification function in the absence of oxygen. These autotrophic bacteria synthesize and grow cells from the energy generated when hydrogen and reducing sulfur compounds are oxidized and carbon dioxide in the air, respectively. Although these bacteria are known to have a denitrifying effect because of their low growth rate and weak floc-forming ability, they have hardly been used for denitrification.
【００１８】しかし、発明者らは、これらの独立栄養細
菌が亜硝酸性窒素に対し、従属栄養細菌と比較して極め
て強い耐性を有していることを知見した。すなわち、亜
硝酸性窒素濃度が２０００ｍｇ／ｌに上昇しても、脱窒
素速度の低下は見られなかった。したがって、アンモニ
ア性窒素を高濃度に含む排水処理の場合、脱窒素用の細
菌としては独立栄養細菌を用いた方が処理の安定化をも
たらす（特願平１１−１１７４１０号）。さらに、発明
者らは、独立栄養細菌の中でも、硫黄酸化細菌は、自己
造粒作用を有している場合もあるため、リアクターでの
高濃度化が容易で、処理の高効率化が可能であることを
知見している（特願平１０−１２２７１９号）。However, the inventors have found that these autotrophic bacteria have extremely strong resistance to nitrite nitrogen as compared to heterotrophic bacteria. That is, even if the nitrite nitrogen concentration increased to 2000 mg / l, no decrease in the denitrification rate was observed. Therefore, in the case of wastewater treatment containing a high concentration of ammonia nitrogen, the use of autotrophic bacteria as the bacteria for denitrification leads to more stable treatment (Japanese Patent Application No. 11-117410). Furthermore, among autotrophic bacteria, the sulfur oxidizing bacteria may have a self-granulating effect, so that the concentration can be easily increased in the reactor and the processing efficiency can be increased. (Japanese Patent Application No. 10-122719).
【００１９】このように、亜硝酸性窒素に耐性のある独
立栄養細菌を用いることにより、従来は困難であった高
濃度のアンモニア性窒素を含有する排水の安定処理が可
能となる。As described above, by using an autotrophic bacterium that is resistant to nitrite nitrogen, it is possible to stably treat wastewater containing a high concentration of ammonia nitrogen, which has been difficult in the past.
【００２０】しかし、実際の排水中には、アンモニア性
窒素ばかりでなく、有機物および硫黄化合物が大量に含
まれる場合がある。例えばコークス工場排水は、有機物
としてフェノールを、硫黄化合物としてチオ硫酸、チオ
シアンを高濃度に含有している。このような場合、独立
栄養細菌単独で脱窒素することはできない。硫黄化合物
だけでなく、有機物が大量に存在しているからである。
有機物が大量に存在している場合、通常、従属栄養細菌
が優占種となってしまう。すなわち、無酸素槽において
は、呼吸源である硝酸性窒素をめぐり、従属栄養細菌と
硫黄酸化細菌の競合が生じるが、有機物が大量に存在す
る場合は、硫黄酸化細菌の増殖に阻害が生じるため、こ
の両者をうまく制御する必要がある。However, actual wastewater sometimes contains a large amount of not only ammonia nitrogen but also organic substances and sulfur compounds. For example, coke plant effluent contains high concentrations of phenol as an organic substance and thiosulfuric acid and thiocyan as sulfur compounds. In such a case, autotrophic bacteria alone cannot be denitrified. This is because not only sulfur compounds but also organic substances are present in large amounts.
When large amounts of organic matter are present, heterotrophic bacteria usually become the dominant species. In other words, in anoxic tanks, competition between heterotrophic bacteria and sulfur oxidizing bacteria occurs over nitrate nitrogen, which is a respiratory source, but when large amounts of organic matter are present, growth of sulfur oxidizing bacteria is inhibited. It is necessary to control both well.
【００２１】さらに、好気槽においても、呼吸源である
酸素をめぐり、従属栄養細菌と独立栄養細菌である硝化
細菌、あるいは亜硝酸菌と硝酸菌の競合が生じるため、
この両者の反応もうまく制御する必要がある。Furthermore, even in an aerobic tank, competition between heterotrophic bacteria and autotrophic bacteria nitrifying bacteria, or nitrite bacteria and nitrate bacteria occurs over oxygen as a respiratory source.
The reaction between the two also needs to be well controlled.
【００２２】本発明は、上記課題を解決するものであ
る。The present invention solves the above problems.
【００２３】[0023]
【課題を解決するための手段】本発明の要旨は、次の
（１）〜（１１）である。The gist of the present invention is the following (1) to (11).
【００２４】（１）排水からの生物学的脱窒素方法にお
いて、無酸素槽にて有機物および硫黄化合物を用い、硫
黄酸化細菌により排水中の亜硝酸性窒素および硝酸性窒
素を窒素ガスに還元して排水から窒素を除去することを
特徴とする排水からの窒素の除去方法。(1) In a method of biologically removing nitrogen from wastewater, nitrate nitrogen and nitrate nitrogen in wastewater are reduced to nitrogen gas by sulfur-oxidizing bacteria using organic substances and sulfur compounds in an oxygen-free tank. A method for removing nitrogen from wastewater, comprising removing nitrogen from the wastewater.
【００２５】（２）無酸素槽において、従属栄養細菌お
よび硫黄酸化細菌を併用することを特徴とする前記
（１）の排水からの窒素の除去方法。(2) The method for removing nitrogen from wastewater according to (1), wherein heterotrophic bacteria and sulfur-oxidizing bacteria are used in combination in an anoxic tank.
【００２６】（３）無酸素槽を多段として、従属栄養細
菌と硫黄酸化細菌を棲み分けて用いることを特徴とする
前記（２）の排水からの窒素の除去方法。(3) The method for removing nitrogen from wastewater according to (2), wherein heterotrophic bacteria and sulfur-oxidizing bacteria are used separately by using a multi-stage anoxic tank.
【００２７】（４）無酸素槽の後段に、硝化細菌により
アンモニア性窒素を亜硝酸性窒素および硝酸性窒素に酸
化する好気槽を設け、この処理水を無酸素槽に循環する
ことを特徴とする前記（１）〜（３）のいずれかの排水
からの窒素の除去方法。(4) An aerobic tank for oxidizing ammonia nitrogen to nitrite nitrogen and nitrate nitrogen by nitrifying bacteria is provided downstream of the anoxic tank, and this treated water is circulated to the anoxic tank. The method for removing nitrogen from wastewater according to any one of the above (1) to (3).
【００２８】（５）好気槽を多段として、硝化細菌であ
る亜硝酸菌と硝酸菌を棲み分けて用いることを特徴とす
る前記（４）の排水からの窒素の除去方法。(5) The method for removing nitrogen from wastewater according to the above (4), wherein nitrifying bacteria and nitrifying bacteria, which are nitrifying bacteria, are used separately in a multistage aerobic tank.
【００２９】（６）亜硝酸菌による処理水を硫黄酸化細
菌主体の無酸素槽に循環し、硝酸菌による処理水を従属
栄養細菌主体の無酸素槽に循環することを特徴とする前
記（５）の排水からの窒素の除去方法。(6) The water treated by nitrite is circulated to an anoxic tank mainly containing sulfur oxidizing bacteria, and the water treated by nitric acid is circulated to an anoxic tank mainly containing heterotrophic bacteria. ) Method for removing nitrogen from wastewater.
【００３０】（７）前記（４）〜（６）のいずれかの方
法による処理水をさらに好気槽に通水し、亜硝酸菌およ
び硝酸菌により、残留するアンモニア性窒素および亜硝
酸性窒素を硝酸性窒素まで完全に酸化することを特徴と
する排水からの窒素の除去方法。(7) The treated water according to any of the above (4) to (6) is further passed through an aerobic tank, and the remaining ammoniacal nitrogen and nitrite nitrogen are removed by nitrite and nitrate. A method for removing nitrogen from wastewater, wherein the nitrogen is completely oxidized to nitrate nitrogen.
【００３１】（８）前記（４）〜（７）のいずれかの方
法による処理水を、従属栄養細菌を主体とする無酸素槽
または硫黄酸化細菌を主体とする無酸素槽に通水し、残
留する亜硝酸性窒素および硝酸性窒素を窒素まで還元す
ることを特徴とする排水からの窒素の除去方法。(8) The treated water according to any one of the above (4) to (7) is passed through an anoxic tank mainly containing heterotrophic bacteria or an anoxic tank mainly containing sulfur oxidizing bacteria. A method for removing nitrogen from wastewater, comprising reducing residual nitrite nitrogen and nitrate nitrogen to nitrogen.
【００３２】（９）硫黄酸化細菌として、造粒させた硫
黄酸化細菌または自己造粒作用を有する硫黄酸化細菌を
用いることを特徴とする前記（１）〜（８）のいずれか
の排水からの窒素の除去方法。(9) A granulated sulfur oxidizing bacterium or a sulfur oxidizing bacterium having a self-granulating action is used as the sulfur oxidizing bacterium according to any one of the above (1) to (8). How to remove nitrogen.
【００３３】（１０）無酸素槽および／または好気槽に
膜分離装置またはろ過装置を設置することを特徴とする
前記（１）〜（９）のいずれかの排水からの窒素の除去
方法。(10) The method for removing nitrogen from wastewater according to any one of the above (1) to (9), wherein a membrane separation device or a filtration device is installed in the anoxic tank and / or the aerobic tank.
【００３４】（１１）無酸素槽および／または好気槽に
微生物固定化担体を投入することを特徴とする前記
（１）〜（１０）のいずれかの排水からの窒素の除去方
法。(11) The method for removing nitrogen from wastewater according to any one of (1) to (10), wherein the microorganism-immobilized carrier is put into an anoxic tank and / or an aerobic tank.
【００３５】[0035]
【発明の実施の形態】本発明の処理フローを図１に、各
槽の機能を表１に示す。DESCRIPTION OF THE PREFERRED EMBODIMENTS FIG. 1 shows the processing flow of the present invention, and Table 1 shows the function of each tank.
【００３６】[0036]
【表１】 [Table 1]
【００３７】まず、無酸素槽１では、好気槽４で生成し
た硝酸性窒素を従属栄養細菌を用いて次式のように窒素
ガスまで還元する。窒素の形態としては、大半が硝酸性
窒素となっているため、従属栄養細菌への阻害が少な
い。この状況下では、従属栄養細菌は硫黄酸化細菌より
もはるかに増殖速度が大きいため、従属栄養細菌による
脱窒素が主体となる。First, in the anoxic tank 1, the nitrate nitrogen generated in the aerobic tank 4 is reduced to nitrogen gas using a heterotrophic bacterium as shown in the following equation. As the form of nitrogen is mostly nitrate nitrogen, there is little inhibition on heterotrophic bacteria. In this situation, heterotrophic bacteria have a much higher growth rate than sulfur-oxidizing bacteria, and thus mainly denitrify by heterotrophic bacteria.
【００３８】 ２ＮＯ3 - ＋１０Ｈ2 → Ｎ2 ＋４Ｈ2Ｏ＋２ＯＨ- 2NO 3 − + 10H 2 → N 2 + 4H 2 O + 2OH −
【００３９】次に、無酸素槽２では、好気槽３で生成し
た亜硝酸性窒素を硫黄酸化細菌を用いて次式のように窒
素ガスまで還元する。自己造粒した硫黄酸化細菌を用い
ることが望ましいが、硫黄酸化細菌のかわりに水素細菌
を用いてもかまわない。窒素の形態としては、大半が亜
硝酸性窒素となっているため、従属栄養細菌は生育が困
難である。この状況下では、亜硝酸性窒素に耐性のある
硫黄酸化細菌が優占種となり、硫黄酸化細菌による脱窒
素が主体となる。硫黄源が不足する場合や都市下水など
のようにほとんど硫黄を含まない排水の場合は、チオ硫
酸、硫黄粒などの硫黄源を添加すればよい。排水中の硫
黄と窒素の重量比率（以下、Ｓ／Ｎ比という）が３．５
以上になるように添加することが望ましい。Next, in the anoxic tank 2, the nitrite nitrogen generated in the aerobic tank 3 is reduced to nitrogen gas using sulfur oxidizing bacteria as in the following equation. It is desirable to use self-granulated sulfur oxidizing bacteria, but hydrogen bacteria may be used instead of sulfur oxidizing bacteria. As the form of nitrogen is mostly nitrite nitrogen, heterotrophic bacteria are difficult to grow. In this situation, sulfur oxidizing bacteria resistant to nitrite nitrogen become the dominant species, and denitrification by sulfur oxidizing bacteria is dominant. In the case where the sulfur source is insufficient, or in the case of wastewater containing almost no sulfur such as municipal sewage, a sulfur source such as thiosulfuric acid and sulfur particles may be added. The weight ratio of sulfur to nitrogen in the wastewater (hereinafter referred to as S / N ratio) is 3.5
It is desirable to add so that it becomes above.
【００４０】 ２ＮＯ2 - ＋ ６Ｈ2 → Ｎ2 ＋２Ｈ2Ｏ＋２ＯＨ- 2NO 2 − + 6H 2 → N 2 + 2H 2 O + 2OH −
【００４１】なお、無酸素槽１と無酸素槽２は、排水の
有機物濃度が低い場合は、１つの槽としてもかまわない
ことも新たに知見した。具体的には、排水中の有機物の
指標であるＢＯＤと窒素の重量比率（以下、ＢＯＤ／Ｎ
比という）が１以下の場合、１槽としてもかまわない。
なお、この場合において、Ｓ／Ｎ比は３．５以上あるこ
とが望ましい。このような条件下では、従属栄養細菌も
ある程度存在が可能であるが、返送される亜硝酸性窒素
のため脱窒素機能が大幅に低下しているため、主として
硫黄酸化細菌によって脱窒素反応が進行する。さらに、
この程度の有機物が存在すると、浮遊性有機物に硫黄酸
化細菌が付着したり、わずかに存在する従属栄養細菌か
ら発生する高分子物質により、硫黄酸化細菌の凝集性が
高まり、硫黄酸化細菌の高濃度化が容易となる利点があ
ることがわかった。したがって、排水中にある程度の有
機物濃度があることは硫黄酸化細菌にとって望ましいこ
とである。例えば、都市下水の活性汚泥処理水はＢＯ
Ｄ：２０ｍｇ／ｌ以下と有機物濃度が低く、ＢＯＤ／Ｎ
比が０．４〜１程度であるから、硫黄酸化細菌による１
槽処理が可能である。また、排水中に全く有機物が含ま
れていない場合、このまま硫黄酸化細菌による処理も可
能であるが、メタノールや酢酸等の有機化合物をＢＯＤ
／Ｎ比が０．１〜１程度となるように添加することが望
ましい。It was newly found that the oxygen-free tank 1 and the oxygen-free tank 2 may be used as one tank when the concentration of organic matter in the wastewater is low. Specifically, the weight ratio of BOD to nitrogen (hereinafter referred to as BOD / N
When the ratio is 1 or less, it may be one tank.
In this case, the S / N ratio is desirably 3.5 or more. Under these conditions, heterotrophic bacteria can be present to some extent, but since the nitrite nitrogen is returned, the denitrification function is greatly reduced, and the denitrification reaction proceeds mainly by sulfur-oxidizing bacteria. I do. further,
When such organic matter is present, sulfur-oxidizing bacteria adhere to the planktonic organic matter, and macromolecules generated from slightly existing heterotrophic bacteria increase the cohesiveness of the sulfur-oxidizing bacteria and increase the concentration of sulfur-oxidizing bacteria. It has been found that there is an advantage that the conversion becomes easy. It is therefore desirable for sulfur oxidizing bacteria to have some organic matter concentration in the wastewater. For example, activated sludge treated water of municipal sewage is BO
D: Organic matter concentration as low as 20 mg / l or less, BOD / N
Since the ratio is about 0.4 to 1, 1
Tank treatment is possible. In addition, when no organic matter is contained in the wastewater, treatment with sulfur-oxidizing bacteria is possible as it is, but organic compounds such as methanol and acetic acid can be treated with BOD.
It is desirable to add such that the / N ratio becomes about 0.1 to 1.
【００４２】次に、好気槽３では、亜硝酸菌により次式
のようにアンモニア性窒素を亜硝酸性窒素まで酸化す
る。処理水には亜硝酸が主体で蓄積しており、この処理
水を無酸素槽２に循環する。Next, in the aerobic tank 3, ammonium nitrate is oxidized by nitrite to nitrite nitrogen as shown in the following formula. Nitrite is mainly accumulated in the treated water, and the treated water is circulated to the oxygen-free tank 2.
【００４３】 ２ＮＨ4 + ＋ ３Ｏ2 → ２ＮＯ2 -＋２Ｈ2Ｏ＋４Ｈ+ 2NH 4 + + 3O 2 → 2NO 2 − + 2H 2 O + 4H +
【００４４】さらに、好気槽４では、硝酸菌により次式
のように亜硝酸性窒素を硝酸性窒素まで酸化する。処理
水には硝酸が主体で蓄積しており、この処理水を無酸素
槽１に循環する。Further, in the aerobic tank 4, nitrite nitrogen is oxidized to nitrate nitrogen by a nitric acid bacterium as shown in the following formula. Nitric acid is mainly accumulated in the treated water, and the treated water is circulated to the oxygen-free tank 1.
【００４５】２ＮＯ2 - ＋ Ｏ2 → ２ＮＯ3 - [0045] 2NO 2 - + O 2 → 2NO 3 -
【００４６】このように、脱窒素工程において、亜硝酸
性窒素に耐性のある独立栄養細菌を併用して亜硝酸性窒
素を還元して窒素ガスにする方法を用いると、硝化工程
において、必ずしも亜硝酸性窒素を完全に硝酸性窒素ま
で酸化する必要が無くなり、従来の生物学的硝化−脱窒
素法と比較して、反応槽の処理時間の短縮や維持管理が
容易となる。As described above, in the denitrification step, if the method of reducing nitrite nitrogen to nitrogen gas by using an autotrophic bacterium resistant to nitrite nitrogen is used, the nitrite step is not necessarily required. There is no need to completely oxidize nitrate nitrogen to nitrate nitrogen, which makes it easier to shorten the processing time and maintain the reactor compared to the conventional biological nitrification-denitrification method.
【００４７】なお、先にも述べたように、排水のＢＯＤ
／Ｎ比が１以下の場合は、無酸素槽が１つの場合があ
る。このような場合、硫黄酸化細菌によって脱窒素反応
が進行するため、好気槽も１つでかまわない。As described above, the BOD of wastewater
When the / N ratio is 1 or less, there may be one oxygen-free tank. In such a case, a single aerobic tank may be used because the denitrification reaction proceeds by the sulfur-oxidizing bacteria.
【００４８】さらに、排水の窒素の形態がアンモニア性
窒素ではなく、高濃度の亜硝酸性窒素および／または硝
酸性窒素の場合、好気槽３および好気槽４は必要ない。
この場合、硫黄酸化細菌を単独で用いる無酸素槽２で処
理することが望ましい。Furthermore, if the form of nitrogen in the wastewater is not ammoniacal nitrogen but a high concentration of nitrite nitrogen and / or nitrate nitrogen, the aerobic tanks 3 and 4 are not required.
In this case, it is desirable to treat in an anoxic tank 2 using sulfur oxidizing bacteria alone.
【００４９】さらに、先に述べた方法では循環方式を採
用しているため、循環総量を原水量の４倍とっても最大
窒素除去率は７５％程度である。したがって、さらに除
去率をあげる必要がある場合は、以下のように処理す
る。すなわち、処理水６中の窒素が亜硝酸性窒素および
硝酸性窒素の場合には、無酸素槽８と残留有機物や硫黄
化合物の除去のための好気槽９を設置すればよい。処理
水６中にアンモニア性窒素が残留している場合には、図
１に示したように、好気槽７と無酸素槽８と好気槽９を
設置すればよい。Further, since the circulation method is employed in the above-described method, the maximum nitrogen removal rate is about 75% even if the total circulation amount is four times the raw water amount. Therefore, if it is necessary to further increase the removal rate, the following processing is performed. That is, when the nitrogen in the treated water 6 is nitrite nitrogen and nitrate nitrogen, an anoxic tank 8 and an aerobic tank 9 for removing residual organic substances and sulfur compounds may be provided. When ammoniacal nitrogen remains in the treated water 6, an aerobic tank 7, an anoxic tank 8, and an aerobic tank 9 may be installed as shown in FIG.
【００５０】また、各槽での細菌濃度を高めるために、
自己造粒作用を有する硫黄酸化細菌または凝集剤を併用
して造粒させた硫黄酸化細菌を用いることが好ましい。
さらに、各槽にプラスチックス、セラミックス、スラ
グ、ゲル等の微生物固定化担体を投入して各槽の微生物
を高濃度化することにより、一層の高効率処理が可能と
なる。無酸素槽１、２、好気槽３、４の内部に膜分離装
置を設置したり、各層の出口近辺にろ過装置を設置する
ことにより、それぞれの微生物を高濃度化し、一層の高
効率処理を図ることも可能である。沈殿池５の代わり
に、膜分離装置または濾過装置を設置することもでき
る。In order to increase the bacterial concentration in each tank,
It is preferable to use a sulfur-oxidizing bacterium having a self-granulating action or a sulfur-oxidizing bacterium granulated in combination with a flocculant.
In addition, a microorganism-immobilized carrier such as plastics, ceramics, slag, and gel is charged into each tank to increase the concentration of microorganisms in each tank, so that more efficient treatment can be performed. By installing a membrane separation device inside the anoxic tanks 1 and 2 and the aerobic tanks 3 and 4 and installing a filtration device near the outlet of each layer, the concentration of each microorganism is increased, and further high-efficiency treatment is performed. It is also possible to plan. Instead of the sedimentation basin 5, a membrane separation device or a filtration device can be installed.
【００５１】[0051]
【実施例】本発明の方法を、製鉄所コークス工場から発
生する安水からの有機物および窒素除去に適用した。EXAMPLE The method of the present invention was applied to the removal of organic matter and nitrogen from low-temperature water generated from a steelmaking coke plant.
【００５２】安水はフェノールが主体の排水であるが、
アンモニア性窒素も大量に含んでいるため、アンモニア
ストリッピングによりアンモニア性窒素を９０％程度除
去した後、海水および／または淡水により３〜５倍程度
に希釈し、活性汚泥法によりフェノールを中心に分解除
去していた。このような安水活性汚泥処理水は、活性汚
泥によってフェノール等の有機物は除去されているもの
の、アンモニア性窒素はほとんど除去されず、３００〜
１０００ｍｇ／ｌ程度含有していることが多い。[0052] Ansui is a wastewater mainly composed of phenol.
Since ammonia nitrogen is contained in a large amount, about 90% of ammonia nitrogen is removed by ammonia stripping, and then diluted about 3 to 5 times with seawater and / or fresh water. Had been removed. In such a treated water with activated sludge, although organic substances such as phenol are removed by activated sludge, ammonia nitrogen is hardly removed and 300 to
It often contains about 1000 mg / l.
【００５３】希釈後の安水を対象として、本発明法を適
用した。供給原水の性状を表２に示す。The method of the present invention was applied to the diluted water. Table 2 shows the properties of the feed water.
【００５４】[0054]
【表２】 [Table 2]
【００５５】図１の好気槽３でアンモニア性窒素を亜硝
酸性窒素まで酸化するため、以下の運転条件で運転し
た。好気槽３に浮遊性の円筒型プラスチックス担体（内
径：３ｍｍ；長さ４ｍｍ）を脱窒槽容積あたり１５％投
入し、亜硝酸菌を付着させた。硫酸および水酸化ナトリ
ウムによってｐＨを７．５〜８．５に制御するととも
に、空気および／または酸素によりＤＯを２ｍｇ／ｌ以
上、ＯＲＰを＋１５０ｍＶ（銀／塩化銀基準）以上に維
持するように運転した。ＨＲＴ（水理学的滞留時間）が
１２時間（アンモニア性窒素容積負荷が１．６ｋｇ−Ｎ
／ｍ3・日）の条件で、アンモニア性窒素（８００ｍｇ
／ｌ）は７０％が亜硝酸性窒素に、２０％が硝酸性窒素
となり、アンモニア性窒素も１０％残留した。本液を原
水量に対して３倍量、無酸素槽２に循環した。In order to oxidize ammonia nitrogen to nitrite nitrogen in the aerobic tank 3 shown in FIG. 1, operation was carried out under the following operating conditions. A floating cylindrical plastics carrier (inner diameter: 3 mm; length: 4 mm) was charged into the aerobic tank 3 at 15% per volume of the denitrification tank, and nitrite was allowed to adhere. The pH is controlled to 7.5 to 8.5 by sulfuric acid and sodium hydroxide, and the operation is performed by air and / or oxygen to maintain DO at 2 mg / l or more and ORP at +150 mV (silver / silver chloride standard) or more. did. HRT (hydraulic residence time) is 12 hours (ammonia nitrogen volume load is 1.6 kg-N
/ M 3 · day) under ammonia nitrogen (800 mg
In (l), 70% was in nitrite nitrogen, 20% was in nitrate nitrogen, and 10% of ammonia nitrogen remained. This solution was circulated to the oxygen-free tank 2 in an amount three times the amount of the raw water.
【００５６】無酸素槽２には自己造粒させた硫黄酸化細
菌を投入した。硫黄源１１として、排水中のチオ硫酸と
合算してチオ硫酸が硫黄として亜硝酸性窒素の３．５倍
量になるように添加した。硫酸および水酸化ナトリウム
によってｐＨを７〜８に制御するとともに、ＨＲＴが２
時間（亜硝酸性窒素の容積負荷が１１ｋｇ−Ｎ／ｍ3・
日）の条件で運転した。ここで７５％の除去率が得ら
れ、総窒素濃度は２００ｍｇ／ｌとなった。余分な硫黄
化合物が好気槽３に流入するのを防ぐため、無酸素槽２
のＯＲＰを−２００ｍＶ（銀／塩化銀基準）程度に維持
するよう、空気および／または酸素を間欠的に供給し
た。The anoxic tank 2 was charged with self-granulated sulfur-oxidizing bacteria. As the sulfur source 11, thiosulfuric acid in the wastewater was added so that the total amount of thiosulfuric acid was 3.5 times the amount of nitrite nitrogen as sulfur. The pH is controlled to 7 to 8 with sulfuric acid and sodium hydroxide, and the HRT is 2
Time (volume loading of nitrite nitrogen is 11kg-N / m 3 ·
Day). Here, a removal rate of 75% was obtained, and the total nitrogen concentration was 200 mg / l. In order to prevent excess sulfur compounds from flowing into the aerobic tank 3, the oxygen-free tank 2
And / or oxygen was supplied intermittently to maintain the ORP of about -200 mV (based on silver / silver chloride).
【００５７】好気槽４では、亜硝酸性窒素を硝酸性窒素
まで酸化するために以下の運転条件で運転した。好気槽
４にも浮遊性の円筒型プラスチックス担体（内径：３ｍ
ｍ；長さ４ｍｍ）を脱窒槽容積あたり１５％投入し、硝
化菌を付着させた。硫酸および水酸化ナトリウムによっ
てｐＨを７〜８に制御するとともに、空気および／また
は酸素によりＤＯを２ｍｇ／ｌ以上、ＯＲＰを＋２００
ｍＶ（銀／塩化銀基準）以上に維持するように運転し
た。ＨＲＴが６時間（窒素容積負荷が０．８ｋｇ−Ｎ／
ｍ3・日）で、窒素（２００ｍｇ／ｌ）は９５％が硝酸
性窒素となった。亜硝酸性窒素は１０ｍｇ／ｌ程度であ
り、この程度では従属栄養細菌の阻害は生じない。本液
を原水量に対して３倍量、無酸素槽１に循環した。The aerobic tank 4 was operated under the following operating conditions to oxidize nitrite nitrogen to nitrate nitrogen. Floating cylindrical plastics carrier (inner diameter: 3m)
m; 4 mm in length) was added at 15% per denitrification tank volume, and nitrifying bacteria were attached. The pH is controlled to 7 to 8 by sulfuric acid and sodium hydroxide, DO is 2 mg / l or more, and ORP is +200 by air and / or oxygen.
The operation was performed so as to maintain mV (based on silver / silver chloride). HRT for 6 hours (nitrogen volume load is 0.8kg-N /
m 3 · day), 95% of nitrogen (200 mg / l) became nitrate nitrogen. The amount of nitrite nitrogen is about 10 mg / l, at which level no inhibition of heterotrophic bacteria occurs. This solution was circulated to the oxygen-free tank 1 in an amount three times the amount of the raw water.
【００５８】無酸素槽１には、下水の活性汚泥などの従
属栄養細菌を投入した。硫酸および水酸化ナトリウムに
よってｐＨを７〜８に制御するとともに、ＨＲＴが４時
間（硝酸性窒素の容積負荷が１．２ｋｇ−Ｎ／ｍ3・
日）の条件で運転した。ここで７５％の除去率が得ら
れ、総窒素濃度は５０ｍｇ／ｌとなった。余分な有機物
が無酸素槽２に流入するのを防ぐため、無酸素槽１のＯ
ＲＰを−２００ｍＶ（銀／塩化銀基準）程度に維持する
よう、空気および／または酸素を間欠的に供給した。Into the anoxic tank 1, heterotrophic bacteria such as activated sludge of sewage were charged. The pH is controlled to 7 to 8 with sulfuric acid and sodium hydroxide, and the HRT is maintained for 4 hours (the volumetric load of nitrate nitrogen is 1.2 kg-N / m 3 ···
Day). Here, a removal rate of 75% was obtained, and the total nitrogen concentration was 50 mg / l. In order to prevent excess organic matter from flowing into the anaerobic tank 2, the O
Air and / or oxygen were intermittently supplied to maintain the RP at about -200 mV (based on silver / silver chloride).
【００５９】好気槽４の後段には沈殿池５を設置し、微
生物と処理水６を分離し、沈殿濃縮した微生物群は無酸
素槽１に返送した。A sedimentation basin 5 was installed at the subsequent stage of the aerobic tank 4, and the microorganisms and the treated water 6 were separated. The microorganisms precipitated and concentrated were returned to the anoxic tank 1.
【００６０】窒素放流基準が平均６０ｍｇ／ｌの場合、
ここまでの処理で十分である。しかし、さらにより高度
な水質が求められる場合は、以下の工程を加えた。When the nitrogen release standard is 60 mg / l on average,
The processing up to this point is sufficient. However, if even higher water quality was required, the following steps were added.
【００６１】処理水６を、後段にサドル型のセラミック
ス（サイズ：１インチ）を好気槽容量あたり７０％充填
した好気槽７に通水した。硫酸および水酸化ナトリウム
によってｐＨを７〜８に制御するとともに、空気および
／または酸素によりＤＯを２ｍｇ／ｌ以上、ＯＲＰを＋
２００ｍＶ（銀／塩化銀基準）以上に維持するように運
転した。ＨＲＴが１時間で、窒素（５０ｍｇ／ｌ）は完
全に硝酸性窒素となった。The treated water 6 was passed through an aerobic tank 7 in which a saddle-type ceramic (size: 1 inch) was filled 70% per aerobic tank capacity in the latter stage. The pH is controlled to 7 to 8 by sulfuric acid and sodium hydroxide, DO is 2 mg / l or more, and ORP is ++ by air and / or oxygen.
The operation was performed so as to maintain 200 mV (based on silver / silver chloride). At an HRT of 1 hour, the nitrogen (50 mg / l) was completely turned into nitrate nitrogen.
【００６２】さらに、無酸素槽８には硫黄酸化細菌を投
入し、硫黄源１１としてチオ硫酸を硫黄として残留窒素
の３倍量添加し、上向流れで通水した。無酸素槽８の上
部には、浮遊性の円筒型プラスチックス担体（内径：３
ｍｍ；長さ４ｍｍ）を無酸素槽８の容積あたり２５％投
入した。また、無酸素槽８の下部中央に水中攪拌機を設
置し、常時攪拌することにより、プラスチックス担体に
浮上した硫黄酸化細菌が固着することを防止した。硫酸
および水酸化ナトリウムによってｐＨを７〜８に制御す
るとともに、ＨＲＴが１時間（窒素容積負荷が１．２ｋ
ｇ−Ｎ／ｍ3・日）の条件で運転したが、処理水中の窒
素濃度は５ｍｇ／ｌ以下となった。Further, a sulfur-oxidizing bacterium was introduced into the anoxic tank 8, thiosulfuric acid was added as a sulfur source 11 in the amount of three times the amount of residual nitrogen as sulfur, and water was passed in an upward flow. Above the oxygen-free tank 8, a floating cylindrical plastic carrier (inner diameter: 3
mm; length 4 mm) was charged at 25% per volume of the oxygen-free tank 8. In addition, an underwater stirrer was installed at the center of the lower part of the anoxic tank 8 to constantly stir to prevent the sulfur-oxidizing bacteria floating on the plastics carrier from sticking. The pH is controlled to 7 to 8 with sulfuric acid and sodium hydroxide, and the HRT is set for 1 hour (nitrogen volume load is 1.2 k
g-N / m 3 · day), but the nitrogen concentration in the treated water became 5 mg / l or less.
【００６３】さらに、処理水中に残留するチオ硫酸は、
好気槽９において硫酸イオンまで酸化した。好気槽９に
は好気性硫黄酸化細菌を投入し、曝気によって溶存酸素
を２ｍｇ／ｌ以上に維持した。ＨＲＴ１時間でチオ硫酸
は硫酸イオンまで完全に酸化され、ＢＯＤも２０ｍｇ／
ｌ以下となった。Further, thiosulfuric acid remaining in the treated water is:
In the aerobic tank 9, it was oxidized to sulfate ions. The aerobic tank 9 was charged with aerobic sulfur-oxidizing bacteria, and the dissolved oxygen was maintained at 2 mg / l or more by aeration. Thiosulfuric acid was completely oxidized to sulfate ions in 1 hour of HRT, and BOD was 20 mg /
1 or less.
【００６４】以上の方法により、最終処理水１０のＢＯ
Ｄは２０ｍｇ／ｌ以下、窒素は５ｍｇ／ｌ以下となっ
た。By the above method, the BO of the final treated water 10
D was 20 mg / l or less, and nitrogen was 5 mg / l or less.
【００６５】[0065]
【発明の効果】本発明により、有機物とアンモニア性窒
素を高濃度に含有する排水から、安定した窒素除去が可
能となる。According to the present invention, stable removal of nitrogen from wastewater containing high concentrations of organic substances and ammoniacal nitrogen can be achieved.
【図１】本発明の処理フローを示す図である。FIG. 1 is a diagram showing a processing flow of the present invention.
１ 無酸素槽 ２ 無酸素槽 ３ 好気槽 ４ 好気槽 ５ 沈殿池 ６ 処理水 ７ 好気槽 ８ 無酸素槽 ９ 好気槽 １０ 最終処理水 １１ 硫黄源 1 Anoxic tank 2 Anoxic tank 3 Aerobic tank 4 Aerobic tank 5 Sedimentation basin 6 Treated water 7 Aerobic tank 8 Anoxic tank 9 Aerobic tank 10 Final treated water 11 Sulfur source
Claims (11)
て、無酸素槽にて有機物および硫黄化合物を用い、硫黄
酸化細菌により排水中の亜硝酸性窒素および硝酸性窒素
を窒素ガスに還元して排水から窒素を除去することを特
徴とする排水からの窒素の除去方法。1. A method for biological denitrification from wastewater, wherein organic substances and sulfur compounds are used in an oxygen-free tank, and nitrite nitrogen and nitrate nitrogen in the wastewater are reduced to nitrogen gas by sulfur oxidizing bacteria. A method for removing nitrogen from wastewater, comprising removing nitrogen from wastewater.
硫黄酸化細菌を併用することを特徴とする請求項１記載
の排水からの窒素の除去方法。2. The method for removing nitrogen from wastewater according to claim 1, wherein heterotrophic bacteria and sulfur-oxidizing bacteria are used together in the anoxic tank.
硫黄酸化細菌を棲み分けて用いることを特徴とする請求
項２記載の排水からの窒素の除去方法。3. The method for removing nitrogen from wastewater according to claim 2, wherein the oxygen-free tank is provided in multiple stages, and heterotrophic bacteria and sulfur-oxidizing bacteria are used separately.
モニア性窒素を亜硝酸性窒素および硝酸性窒素に酸化す
る好気槽を設け、この処理水を無酸素槽に循環すること
を特徴とする請求項１〜３のいずれかに記載の排水から
の窒素の除去方法。4. An aerobic tank for oxidizing ammonia nitrogen to nitrite nitrogen and nitrate nitrogen by nitrifying bacteria is provided at a stage subsequent to the anoxic tank, and the treated water is circulated to the anoxic tank. The method for removing nitrogen from wastewater according to claim 1.
硝酸菌と硝酸菌を棲み分けて用いることを特徴とする請
求項４記載の排水からの窒素の除去方法。5. The method for removing nitrogen from wastewater according to claim 4, wherein the aerobic tank is provided in multiple stages, and nitrifying bacteria and nitrifying bacteria which are nitrifying bacteria are used separately.
体の無酸素槽に循環し、硝酸菌による処理水を従属栄養
細菌主体の無酸素槽に循環することを特徴とする請求項
５記載の排水からの窒素の除去方法。6. The water treated by nitrite is circulated to an anoxic tank mainly containing sulfur oxidizing bacteria, and the water treated by nitric acid is circulated to an anoxic tank mainly containing heterotrophic bacteria. For removing nitrogen from effluents of wastewater.
よる処理水をさらに好気槽に通水し、亜硝酸菌および硝
酸菌により、残留するアンモニア性窒素および亜硝酸性
窒素を硝酸性窒素まで完全に酸化することを特徴とする
排水からの窒素の除去方法。7. The treated water according to any one of claims 4 to 6 is further passed through an aerobic tank, and the remaining ammoniacal nitrogen and nitrite nitrogen are removed by nitrite and nitrate. A method for removing nitrogen from wastewater, wherein the nitrogen is completely oxidized to neutral nitrogen.
よる処理水を、従属栄養細菌を主体とする無酸素槽また
は硫黄酸化細菌を主体とする無酸素槽に通水し、残留す
る亜硝酸性窒素および硝酸性窒素を窒素まで還元するこ
とを特徴とする排水からの窒素の除去方法。8. The treated water according to any one of claims 4 to 7 is passed through an anoxic tank mainly composed of heterotrophic bacteria or an anoxic tank mainly composed of sulfur oxidizing bacteria, and remains. A method for removing nitrogen from wastewater, comprising reducing nitrite nitrogen and nitrate nitrogen to nitrogen.
化細菌または自己造粒作用を有する硫黄酸化細菌を用い
ることを特徴とする請求項１〜８のいずれかに記載の排
水からの窒素の除去方法。9. The method according to claim 1, wherein a granulated sulfur oxidizing bacterium or a sulfur oxidizing bacterium having a self-granulating action is used as the sulfur oxidizing bacterium. Removal method.
離装置またはろ過装置を設置することを特徴とする請求
項１〜９のいずれかに記載の排水からの窒素の除去方
法。10. The method for removing nitrogen from wastewater according to claim 1, wherein a membrane separation device or a filtration device is installed in the anoxic tank and / or the aerobic tank.
物固定化担体を投入することを特徴とする請求項１〜１
０のいずれかに記載の排水からの窒素の除去方法。11. The microorganism-immobilized carrier is introduced into an anoxic tank and / or an aerobic tank.
0. The method for removing nitrogen from wastewater according to any one of 0.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25968499A JP3958900B2 (en) | 1999-09-14 | 1999-09-14 | How to remove nitrogen from wastewater |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP25968499A JP3958900B2 (en) | 1999-09-14 | 1999-09-14 | How to remove nitrogen from wastewater |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2001079593A true JP2001079593A (en) | 2001-03-27 |
| JP3958900B2 JP3958900B2 (en) | 2007-08-15 |
Family
ID=17337488
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP25968499A Expired - Fee Related JP3958900B2 (en) | 1999-09-14 | 1999-09-14 | How to remove nitrogen from wastewater |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3958900B2 (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2369115A (en) * | 2000-11-17 | 2002-05-22 | Kwangju Inst Sci & Tech | Simultaneous removal process of nitrogen and phosphorus in wastewater |
| JP2005211832A (en) * | 2004-01-30 | 2005-08-11 | Nippon Steel Corp | Method for removing ammonia nitrogen from waste water |
| KR100970576B1 (en) * | 2008-01-22 | 2010-07-16 | 강원대학교산학협력단 | The apparatus and method of removing BOD, N, and P removal from an animal wastewater |
| WO2011103286A2 (en) * | 2010-02-17 | 2011-08-25 | University Of South Florida | Solids retention time uncoupling by selective wasting of sludge |
| JP2016077954A (en) * | 2014-10-15 | 2016-05-16 | 新日鐵住金株式会社 | Biological nitrogen removal method |
| CN111979138A (en) * | 2020-05-21 | 2020-11-24 | 厦门大学 | Heterotrophic nitrification aerobic denitrifying bacterium Y15 and application thereof |
| CN113121015A (en) * | 2021-05-21 | 2021-07-16 | 哈尔滨工业大学（深圳） | Water treatment device |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| CN102249492B (en) * | 2011-06-20 | 2012-12-26 | 北京桑德环境工程有限公司 | Processing method of lamivudine wastewater |
| CN104355404B (en) * | 2014-10-27 | 2017-03-01 | 北京工业大学 | A kind of method and apparatus quickly realizing biofilter Anammox |
-
1999
- 1999-09-14 JP JP25968499A patent/JP3958900B2/en not_active Expired - Fee Related
Cited By (12)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB2369115A (en) * | 2000-11-17 | 2002-05-22 | Kwangju Inst Sci & Tech | Simultaneous removal process of nitrogen and phosphorus in wastewater |
| GB2369115B (en) * | 2000-11-17 | 2003-01-08 | Kwangju Inst Sci & Tech | Simultaneous removal process of nitrogen and phosphorous in wastewater |
| JP2005211832A (en) * | 2004-01-30 | 2005-08-11 | Nippon Steel Corp | Method for removing ammonia nitrogen from waste water |
| JP4570069B2 (en) * | 2004-01-30 | 2010-10-27 | 新日本製鐵株式会社 | Method for removing ammonia nitrogen from wastewater |
| KR100970576B1 (en) * | 2008-01-22 | 2010-07-16 | 강원대학교산학협력단 | The apparatus and method of removing BOD, N, and P removal from an animal wastewater |
| WO2011103286A2 (en) * | 2010-02-17 | 2011-08-25 | University Of South Florida | Solids retention time uncoupling by selective wasting of sludge |
| WO2011103286A3 (en) * | 2010-02-17 | 2011-12-22 | University Of South Florida | Solids retention time uncoupling by selective wasting of sludge |
| US8535534B2 (en) | 2010-02-17 | 2013-09-17 | University Of South Florida | Solids retention time uncoupling by selective wasting of sludge |
| JP2016077954A (en) * | 2014-10-15 | 2016-05-16 | 新日鐵住金株式会社 | Biological nitrogen removal method |
| CN111979138A (en) * | 2020-05-21 | 2020-11-24 | 厦门大学 | Heterotrophic nitrification aerobic denitrifying bacterium Y15 and application thereof |
| CN111979138B (en) * | 2020-05-21 | 2022-06-21 | 厦门大学 | Heterotrophic nitrification aerobic denitrifying bacterium Y15 and application thereof |
| CN113121015A (en) * | 2021-05-21 | 2021-07-16 | 哈尔滨工业大学（深圳） | Water treatment device |
Also Published As
| Publication number | Publication date |
|---|---|
| JP3958900B2 (en) | 2007-08-15 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CN108483655B (en) | Method for deep denitrification by coupling shortcut nitrification and denitrification with anaerobic ammonia oxidation and sulfur autotrophic denitrification | |
| JP3737410B2 (en) | High concentration organic wastewater treatment method and apparatus using biomaker | |
| JP5100091B2 (en) | Water treatment method | |
| CN112456643A (en) | System and method for realizing partial anaerobic ammonia oxidation deep nitrogen and phosphorus removal by circulating and alternately utilizing main flow and side flow zone biomembrane of urban sewage treatment plant | |
| JP4106203B2 (en) | How to remove nitrogen from water | |
| WO2006022539A1 (en) | Progress for the biological denitrification of ammonium containing wastewater | |
| JP4734996B2 (en) | Biological treatment method and apparatus for nitrogen-containing water | |
| JPH08192185A (en) | Biologically nitrifying and denitrifying method | |
| JP3925902B2 (en) | Biological nitrogen removal method and apparatus | |
| JP2002011495A (en) | Method for removing nitrogen and phosphor from wastewater | |
| JP4302341B2 (en) | Biological nitrogen removal method and apparatus | |
| JP4570069B2 (en) | Method for removing ammonia nitrogen from wastewater | |
| JP3958900B2 (en) | How to remove nitrogen from wastewater | |
| JP2004230338A (en) | Method for removing ammonia nitrogen compound from waste water | |
| JP2003053384A (en) | Method for removing nitrogen and phosphorus from waste water and facility therefor | |
| KR102144118B1 (en) | Method for Removing Nitrogen and Phosphorus from Wastewater by Nutrient Removal Process via Nitrite and by Combining Anaerobic Ammonium Oxidation(ANAMMOX) Process | |
| JP2000308900A (en) | Treatment of ammonia-containing waste water | |
| JP5722087B2 (en) | Biological nitrogen treatment method of ammonia containing wastewater | |
| JP6491056B2 (en) | Nitrogen removal method and nitrogen removal apparatus | |
| JP2007117842A (en) | Method and apparatus for removing nitrogen of high concentration organic waste water | |
| JPH08141597A (en) | Apparatus for treating waste water containing nitrogen and fluorine | |
| CN112408699B (en) | Integrated denitrification method for wastewater containing toxic and harmful organic matters | |
| JP2001212592A (en) | Method for removing nitrogen from wastewater | |
| JP4031597B2 (en) | How to remove nitrogen from wastewater | |
| JP2003071490A (en) | Method for removing nitrogen from wastewater |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A977 | Report on retrieval |
Free format text: JAPANESE INTERMEDIATE CODE: A971007 Effective date: 20050627 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A821 Effective date: 20061228 |
|
| RD02 | Notification of acceptance of power of attorney |
Free format text: JAPANESE INTERMEDIATE CODE: A7422 Effective date: 20061228 |
|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20070206 |
|
| A521 | Written amendment |
Free format text: JAPANESE INTERMEDIATE CODE: A523 Effective date: 20070409 |
|
| TRDD | Decision of grant or rejection written | ||
| A01 | Written decision to grant a patent or to grant a registration (utility model) |
Free format text: JAPANESE INTERMEDIATE CODE: A01 Effective date: 20070508 |
|
| A61 | First payment of annual fees (during grant procedure) |
Free format text: JAPANESE INTERMEDIATE CODE: A61 Effective date: 20070511 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20100518 Year of fee payment: 3 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20110518 Year of fee payment: 4 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20120518 Year of fee payment: 5 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130518 Year of fee payment: 6 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130518 Year of fee payment: 6 |
|
| S531 | Written request for registration of change of domicile |
Free format text: JAPANESE INTERMEDIATE CODE: R313531 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130518 Year of fee payment: 6 |
|
| S533 | Written request for registration of change of name |
Free format text: JAPANESE INTERMEDIATE CODE: R313533 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20130518 Year of fee payment: 6 |
|
| R350 | Written notification of registration of transfer |
Free format text: JAPANESE INTERMEDIATE CODE: R350 |
|
| FPAY | Renewal fee payment (event date is renewal date of database) |
Free format text: PAYMENT UNTIL: 20140518 Year of fee payment: 7 |
|
| LAPS | Cancellation because of no payment of annual fees |