JP2000308895A - Treatment of organic sewage - Google Patents
Treatment of organic sewageInfo
- Publication number
- JP2000308895A JP2000308895A JP11118270A JP11827099A JP2000308895A JP 2000308895 A JP2000308895 A JP 2000308895A JP 11118270 A JP11118270 A JP 11118270A JP 11827099 A JP11827099 A JP 11827099A JP 2000308895 A JP2000308895 A JP 2000308895A
- Authority
- JP
- Japan
- Prior art keywords
- phosphorus
- ammonia
- sludge
- biological treatment
- activated sludge
- 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.)
- Withdrawn
Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Activated Sludge Processes (AREA)
- Removal Of Specific Substances (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、し尿系汚水、工場
廃水、下水などの有機性汚水の処理方法に関し、更に詳
しくは、有機性汚水中のリン、アンモニアを資源回収す
ることができ、かつ生物処理にともなって発生する余剰
汚泥量を減少することができる有機性汚水の処理方法に
関する。The present invention relates to a method for treating organic wastewater such as human wastewater, industrial wastewater, and sewage, and more particularly to a method for recovering phosphorus and ammonia from organic wastewater, and The present invention relates to a method for treating organic wastewater, which can reduce the amount of excess sludge generated during biological treatment.
【０００２】[0002]
【従来の技術】下水などの有機性汚水中の汚染物質の一
つとしてリンがある。該汚水中のリンを除去する技術と
して種々研究開発されている。中でも、有機性汚水を脱
リン処理する有効な方法の１つとして、活性汚泥法の曝
気槽等の生物処理工程に無機凝集剤を添加してリンを除
去する「凝集剤添加活性汚泥法」が知られている。しか
し、これらの方法では有機性汚水中のリン、アンモニア
を資源として回収することができなかった。また、リン
を凝集させた凝集汚泥の発生量が多量であるため、汚泥
処理に大きな負担を与えていた。更に、生物処理工程で
発生する余剰活性汚泥の発生量も多量であり、その処理
処分に苦慮しているのが実情である。アンモニアの除去
法として代表的な生物学的脱窒素法はアンモニアを窒素
ガスとして放出してしまうため窒素資源を回収できなか
った。また運転管理が面倒であり、硝化速度が小さいた
め生物処理槽の所要容積が過大であった。2. Description of the Related Art Phosphorus is one of the pollutants in organic wastewater such as sewage. Various researches and developments have been made on technologies for removing phosphorus from the wastewater. Among them, as one of the effective methods for dephosphorizing organic sewage, there is a "coagulant-added activated sludge method" in which an inorganic coagulant is added to a biological treatment process such as an aeration tank of an activated sludge method to remove phosphorus. Are known. However, these methods could not recover phosphorus and ammonia in organic wastewater as resources. In addition, since the amount of coagulated sludge obtained by coagulating phosphorus is large, a large burden is imposed on the sludge treatment. Furthermore, the amount of surplus activated sludge generated in the biological treatment process is also large, and it is a fact that it is difficult to dispose of it. As a typical method for removing ammonia, a biological denitrification method releases ammonia as nitrogen gas, and thus cannot recover nitrogen resources. Moreover, operation management was troublesome, and the nitrification rate was low, so that the required volume of the biological treatment tank was excessive.
【０００３】[0003]
【発明が解決しようとする課題】本発明は、「凝集剤添
加活性汚泥法」に新規着想を加えたもので、本発明の目
的は、上記の従来技術の課題を解決することにある。有
機性汚水からリン、アンモニアを除去し、且つ貴重な資
源として回収できるようにし、凝集汚泥及び余剰汚泥の
発生量を大きく減少でき、更に無機凝集剤の使用量も削
減できるような有機性汚水の処理方法を提供する。The object of the present invention is to add a new idea to the "coagulant-added activated sludge method", and an object of the present invention is to solve the above-mentioned problems of the prior art. Organic sewage that removes phosphorus and ammonia from organic sewage and can be recovered as a valuable resource, can greatly reduce the amount of coagulated sludge and excess sludge, and can also reduce the amount of inorganic coagulant used. Provide a processing method.
【０００４】[0004]
【課題を解決するための手段】本発明は、以下の手段に
より上記の課題を達成した。 （１）リン、アンモニアを含む有機性汚水を生物処理す
る際に、水酸化鉄、ゼオライトを共存させて、リン、ア
ンモニアを吸着除去する生物処理工程Ａと、生物処理工
程Ａの活性汚泥の一部を引抜いてアルカリ剤を添加し、
該活性汚泥からリン、アンモニアを溶出させ、且つ該活
性汚泥を可溶化し、その後固液分離する工程Ｂと、該固
液分離からの分離液にマグネシウム化合物を添加してリ
ン及びアンモニアをリン酸マグネシウムアンモニウムと
して回収する工程Ｃを有することを特徴とする有機性汚
水の処理方法。 （２）前記Ｂ工程で固液分離により得た分離汚泥を共存
する水酸化鉄、ゼオライトとともに、前記生物処理工程
Ａに供給することを特徴とする請求項１記載の有機性汚
水の処理方法。According to the present invention, the above objects have been attained by the following means. (1) When biologically treating organic wastewater containing phosphorus and ammonia, a biological treatment step A in which iron hydroxide and zeolite coexist to adsorb and remove phosphorus and ammonia, and one of activated sludge in the biological treatment step A Pull out the part and add the alkaline agent,
A step B of eluting phosphorus and ammonia from the activated sludge and solubilizing the activated sludge and then solid-liquid separation, and adding a magnesium compound to the separated liquid from the solid-liquid separation to convert phosphorus and ammonia into phosphoric acid A method for treating organic wastewater, comprising a step C of recovering as magnesium ammonium. (2) The method for treating organic wastewater according to claim 1, wherein the separated sludge obtained by the solid-liquid separation in the step B is supplied to the biological treatment step A together with coexisting iron hydroxide and zeolite.
【０００５】上記の本発明の構成により、以下のような
作用が生ずる。本発明においては、生物処理工程Ａにお
いて、水酸化鉄とゼオライトが共存することにより、有
機性汚水中のリンが水酸化鉄に吸着され、またアンモニ
アがゼオライトに高速に吸着されて活性汚泥とともに沈
殿分離される。その後、工程Ｂにおいてアルカリ処理に
よってリンとアンモニアが沈殿汚泥から溶出され、さら
に工程Ｃで、マグネシウム化合物の添加によって該溶出
液からリンがリン酸マグネシウムアンモニウム（ＭＡ
Ｐ）として回収される。これにより、有機性汚水中のリ
ンを有効に除去し、リンを資源として回収できるように
なる。その際アンモニアも固定され、液から分離され
る。生物汚泥はアルカリによって加水分解され、大部分
は可溶化してＢＯＤ成分に変わる。これを曝気槽等の生
物処理工程に供給すると、該ＢＯＤは分解されるので、
余剰汚泥発生量が減少する。[0005] The above-described configuration of the present invention has the following effects. In the present invention, in the biological treatment step A, the coexistence of iron hydroxide and zeolite allows phosphorus in the organic wastewater to be adsorbed on the iron hydroxide, and ammonia is rapidly adsorbed on the zeolite to precipitate with activated sludge. Separated. Thereafter, in step B, phosphorus and ammonia are eluted from the settled sludge by alkali treatment, and in step C, phosphorus is added from the eluate to magnesium ammonium phosphate (MA) by the addition of a magnesium compound.
Collected as P). Thereby, the phosphorus in the organic sewage can be effectively removed, and the phosphorus can be recovered as a resource. At that time, the ammonia is also fixed and separated from the liquid. Biosludge is hydrolyzed by alkali and is largely solubilized and converted to BOD components. When this is supplied to a biological treatment process such as an aeration tank, the BOD is decomposed,
Excess sludge generation is reduced.
【０００６】また、本発明においては水酸化鉄やゼオラ
イト微粒子を用いることにより、リン、アンモニアは、
この水酸化鉄やゼオライト微粒子にいったん吸着させ
る。その後、アルカリ処理により、リン、アンモニアを
溶出・脱着させる。リンが溶出した水酸化鉄及びアンモ
ニアが脱着したゼオライトは、生物処理工程にリサイク
ルする。これによってリン、アンモニアの吸着に再利用
することができる。新しい、水酸化鉄、ゼオライトの補
充必要量は大きく減少し、ランニングコストが低減でき
る。In the present invention, the use of iron hydroxide or zeolite fine particles allows phosphorus and ammonia to be
The iron hydroxide and the zeolite particles are once adsorbed. Thereafter, phosphorus and ammonia are eluted and desorbed by alkali treatment. The zeolite to which phosphorus hydroxide has been eluted and the iron hydroxide to which ammonia has been desorbed is recycled to the biological treatment step. Thereby, it can be reused for the adsorption of phosphorus and ammonia. The required replenishment of new iron hydroxide and zeolite is greatly reduced, and running costs can be reduced.
【０００７】[0007]
【発明の実施の形態】図１は、本発明の方法の一実施態
様を示す概念図である。以下、図１を参照しながら本発
明を詳しく説明する。本発明の方法の一態様を示した図
１に示すように、生物処理工程Ａとしての生物処理用曝
気槽１と、沈殿槽２と、リン、アンモニア回収手段であ
る脱着槽３、固液分離部４、ＭＡＰ生成槽５、固液分離
部６とからなる方法について説明する。生物処理として
は通常の活性汚泥法、生物膜法、ゲル等の微生物固定化
担体を用いる方法等を適用することができる。FIG. 1 is a conceptual diagram showing one embodiment of the method of the present invention. Hereinafter, the present invention will be described in detail with reference to FIG. As shown in FIG. 1 showing one embodiment of the method of the present invention, an aeration tank 1 for biological treatment as a biological treatment step A, a sedimentation tank 2, a desorption tank 3 as a phosphorus and ammonia recovery means, a solid-liquid separation, The method including the section 4, the MAP generation tank 5, and the solid-liquid separation section 6 will be described. As the biological treatment, an ordinary activated sludge method, a biofilm method, a method using a microorganism-immobilized carrier such as a gel, or the like can be applied.
【０００８】有機性汚水１１は、曝気槽１に導入され、
曝気槽１には水酸化鉄微粒子、ゼオライト微粒子１２が
添加され、有機性汚水１１中のリン、アンモニアが吸着
によって除去される。ここで、水酸化鉄微粒子としては
ＦｅＣｌ3 、Ｆｅ2(ＳＯ4)3、ＦｅＳＯ4 、ポリ硫酸鉄
（ポリ鉄）等にアルカリを添加して生成させた水酸化第
２鉄微粒子が挙げられる。なお塩化第２鉄などの鉄塩を
汚水に添加して汚水中のアルカリ度を利用して水酸化鉄
を生成されるようにしてもよい。ここで、水酸化鉄微粒
子、及びゼオライト微粒子の添加量としては、例えば１
０００〜５０００ｍｇ／リットル程度である。ゼオライ
トは粒径の大きいものを使用すると曝気槽の底に沈殿し
てしまうので、粒径数ミクロンの微粒子を用いる。水酸
化鉄微粒子、ゼオライト微粒子は活性汚泥に共存して沈
殿槽２に送られ、沈殿汚泥１４として沈殿分離され、ま
た処理水１３が分離される。処理水１３はＢＯＤ、Ｓ
Ｓ、リン、アンモニアが除去された清澄な処理水であ
る。The organic sewage 11 is introduced into the aeration tank 1,
Iron hydroxide fine particles and zeolite fine particles 12 are added to the aeration tank 1, and phosphorus and ammonia in the organic wastewater 11 are removed by adsorption. Here, examples of the iron hydroxide fine particles include ferric hydroxide fine particles generated by adding an alkali to FeCl 3 , Fe 2 (SO 4 ) 3 , FeSO 4 , polyiron sulfate (polyiron), or the like. Note that an iron salt such as ferric chloride may be added to the sewage to make use of the alkalinity in the sewage to generate iron hydroxide. Here, the addition amount of the iron hydroxide fine particles and the zeolite fine particles is, for example, 1
It is about 000-5000 mg / liter. If a zeolite having a large particle size is used, it will precipitate at the bottom of the aeration tank. Therefore, fine particles having a particle size of several microns are used. The iron hydroxide fine particles and the zeolite fine particles coexist with the activated sludge and are sent to the sedimentation tank 2, where they are separated as sedimented sludge 14 and the treated water 13 is separated. Treated water 13 is BOD, S
It is clear treated water from which S, phosphorus and ammonia have been removed.
【０００９】分離汚泥１４の大部分は返送汚泥１５とし
て曝気槽１に返送される。それ以外のリン、アンモニア
回収対象である回収汚泥１６は、カセイソーダ等のアル
カリ１７の添加を受けてリン、アンモニアは脱着槽３に
流入する。ここで、アルカリとしては、水酸化ナトリウ
ム、水酸化カリウム等を挙げることができる。このアル
カリをリン、アンモニア脱着槽３へｐＨが１０以上好ま
しくは１１になるよう添加する。リン、アンモニア脱着
槽３では、回収汚泥１６で水酸化鉄に吸着されていたリ
ンがアルカリ性条件にされることによって液側に溶出す
る。ゼオライトに吸着されていたアンモニアもアルカリ
条件下で脱着する。さらに回収汚泥１６に含まれる生物
汚泥が加水分解を受けて可溶化する。該生物汚泥の可溶
化を更に促進するには温度５０℃以上に加温するのが好
ましい。リン、アンモニア脱着槽３の温度は０〜９０℃
が好ましく、ｐＨは１０〜１２が好ましい。滞留時間は
１〜６時間程度が好ましい。尚、曝気槽１の汚泥の一部
を引き抜いてオゾン処理してから曝気槽１に返送する
と、水酸化鉄、ゼオライトのオゾン酸化の触媒効果のた
めか、余剰汚泥の減量効果が顕著に起きることが判っ
た。Most of the separated sludge 14 is returned to the aeration tank 1 as returned sludge 15. Recovered sludge 16 from which phosphorus and ammonia are to be recovered receives the addition of alkali 17 such as caustic soda, and phosphorus and ammonia flow into the desorption tank 3. Here, examples of the alkali include sodium hydroxide and potassium hydroxide. This alkali is added to the phosphorus / ammonia desorption tank 3 so that the pH becomes 10 or more, preferably 11. In the phosphorus / ammonia desorption tank 3, the phosphorus adsorbed on the iron hydroxide in the recovered sludge 16 is eluted to the liquid side by the alkaline condition. Ammonia adsorbed on zeolite also desorbs under alkaline conditions. Further, the biological sludge contained in the recovered sludge 16 is hydrolyzed and solubilized. In order to further promote the solubilization of the biological sludge, it is preferable to heat the temperature to 50 ° C. or higher. The temperature of the phosphorus and ammonia desorption tank 3 is 0 to 90 ° C
Is preferred, and the pH is preferably 10-12. The residence time is preferably about 1 to 6 hours. When a part of the sludge in the aeration tank 1 is withdrawn and treated with ozone, and then returned to the aeration tank 1, the effect of reducing the amount of surplus sludge is remarkable due to the catalytic effect of ozone oxidation of iron hydroxide and zeolite. I understood.
【００１０】リン、アンモニア脱着槽３に供給する回収
汚泥１６の流量ｑは、有機性汚水１１（流量Ｑ）中のリ
ン濃度をＣとし、回収汚泥１６中に含まれるリン含有率
をａとすると、概略ｑ≒ＱＣ／ａに設定すればよい。リ
ン、アンモニア脱着槽３からの流出スラリは、遠心分離
機などの固液分離部４に於いて分離液１８と分離汚泥１
９に分離される。分離液１８にはＭＡＰ生成槽５におい
てマグネシウム化合物２０が添加される。これにより
（ＭＡＰ）リン酸マグネシウムアンモニウム沈殿が析出
する。この沈殿を固液分離部６において分離し、リン資
源２１として回収する。ここで、マグネシウム化合物２
０としては、ＭｇＣｌ2 、ＭｇＳＯ4 、Ｍｇ（Ｏ
Ｈ）2 、ＭｇＯなどが挙げられる。尚ＭＡＰ生成のため
にリン分が不足する場合はマグネシウムとともにリン酸
化合物（リン酸ナトリウムなど）を添加する。ＭＡＰ生
成槽５の滞留時間は３０分〜１時間で充分である。ＭＡ
Ｐ生成槽５に添加するマグネシウム、リン化合物の量
は、分離液１８のなかのアンモニア濃度に対しモル比で
１〜１．５倍で良い。また、ＭＡＰ生成の適正ｐＨは９
〜１０．５であるので、この範囲にｐＨ調整することが
好ましい。The flow rate q of the recovered sludge 16 to be supplied to the phosphorus / ammonia desorption tank 3 is as follows: C is the concentration of phosphorus in the organic waste water 11 (flow rate Q), and a is the phosphorus content contained in the recovered sludge 16. , Approximately q ≒ QC / a. The slurry discharged from the phosphorus / ammonia desorption tank 3 is separated from the separated liquid 18 and separated sludge 1 in the solid-liquid separation section 4 such as a centrifuge.
9 is separated. A magnesium compound 20 is added to the separated liquid 18 in the MAP generation tank 5. This precipitates (MAP) magnesium ammonium phosphate precipitate. This precipitate is separated in the solid-liquid separation section 6 and collected as phosphorus resources 21. Here, magnesium compound 2
As 0, MgCl 2 , MgSO 4 , Mg (O
H) 2 , MgO and the like. If phosphorus content is insufficient due to MAP generation, a phosphoric acid compound (such as sodium phosphate) is added together with magnesium. A residence time in the MAP generation tank 5 of 30 minutes to 1 hour is sufficient. MA
The amount of the magnesium and phosphorus compounds to be added to the P generation tank 5 may be 1 to 1.5 times the molar concentration of the ammonia in the separated liquid 18. The appropriate pH for MAP generation is 9
Therefore, it is preferable to adjust the pH to this range.
【００１１】上記方法において、分離汚泥１９には、リ
ン、アンモニア吸着能力が再生された水酸化鉄微粒子、
ゼオライト微粒子が含まれ、固液分離部６からの分離液
２２には生物汚泥が可溶化したＢＯＤ成分が多量に含ま
れているので、分離汚泥１９と該分離液２２を曝気槽１
に返送すると、生物汚泥の減量化ができる。尚分離汚泥
１９はｐＨ１１程度のアルカリ性であるが量が少ないた
め、そのままｐＨ調製せずに曝気槽１に戻しても特に支
障はなく、生物処理に悪影響を及ぼす心配はない。固液
分離部６はリン酸マグネシウムアンモニウム沈殿の沈降
性が良いので沈殿槽で充分である。In the above method, the separated sludge 19 contains fine particles of iron hydroxide having regenerated phosphorus and ammonia adsorption ability,
Since the zeolite fine particles are contained and the separation liquid 22 from the solid-liquid separation section 6 contains a large amount of the BOD component in which the biological sludge is solubilized, the separation sludge 19 and the separation liquid 22 are separated into the aeration tank 1
When returned to, biological sludge can be reduced. The separated sludge 19 is alkaline at a pH of about 11, but is in a small amount. Therefore, even if the sludge is returned to the aeration tank 1 without adjusting the pH, there is no particular problem, and there is no fear of adversely affecting biological treatment. Since the solid-liquid separation section 6 has good sedimentation of magnesium ammonium phosphate precipitate, a sedimentation tank is sufficient.
【００１２】[0012]
【実施例】以下、実施例を示して、本発明を具体的に説
明するが、本発明の内容がこれらに限定されるものでは
ない。EXAMPLES Hereinafter, the present invention will be described in detail with reference to Examples, but the present invention is not limited thereto.
【００１３】実施例１ 下水（ＢＯＤ１２０ｍｇ／リットル、ＳＳ１１０ｍｇ／
リットル、リンの濃度４．６ｍｇ／リットル、アンモニ
ア性窒素１５．７ｍｇ／リットル）を対象として本発明
の実証試験を行なった。下記第１表にその実験条件を示
した。Example 1 Sewage (BOD 120 mg / liter, SS 110 mg /
Liter, a phosphorus concentration of 4.6 mg / liter, and an ammoniacal nitrogen of 15.7 mg / liter). Table 1 below shows the experimental conditions.
【００１４】[0014]
【表１】 [Table 1]
【００１５】この条件で実験を行なったところ、下水中
のリンが肥料として利用可能なＭＡＰ無水物として、下
水１ｍ3 当たり約２０ｇ回収された。また余剰活性汚泥
発生量は、下水１ｍ3 当たり３９ｇと少量であった。処
理水の水質は、ＢＯＤ５ｍｇ／リットル、ＳＳ８ｍｇ／
リットル、リン濃度０．１２ｍｇ／リットル、アンモニ
ア性窒素０．２ｍｇ／リットルと良好であった。水酸化
ナトリウムの添加量としては、リン脱着槽３のｐＨが１
１になるように設定された。[0015] When an experiment was conducted in this condition, phosphorus in the sewage as an available MAP anhydride as fertilizer, was about 20g collected per sewer 1 m 3. The amount of excess activated sludge generated was as small as 39 g / m 3 of sewage. The quality of the treated water is BOD 5 mg / liter, SS 8 mg /
Liter, the phosphorus concentration was 0.12 mg / liter, and the ammoniacal nitrogen was 0.2 mg / liter. The amount of sodium hydroxide added is such that the pH of the phosphorus desorption tank 3 is 1
It was set to be 1.
【００１６】比較例 通常の標準活性汚泥法により比較実験を行なった。処理
水水質は、ＢＯＤ７ｍｇ／リットル、ＳＳ９ｍｇ／リッ
トル、リン濃度０．４ｍｇ／リットル、アンモニア性窒
素１２ｍｇ／リットルであり、処理水質のリン、アンモ
ニアが本発明より大幅に悪かった。余剰汚泥発生量は下
水１ｍ3 当たり１１０ｇであり、上記実施例１より著し
く多量であった。Comparative Example A comparative experiment was carried out by a standard activated sludge method. The quality of the treated water was 7 mg / L for BOD, 9 mg / L for SS, 0.4 mg / L for phosphorus concentration, and 12 mg / L for ammoniacal nitrogen. The amount of surplus sludge generated was 110 g per m 3 of sewage, which was significantly larger than that in Example 1.
【００１７】[0017]
【発明の効果】本発明によれば、有機性汚水の処理方法
において、有機性汚水からリン、アンモニアを除去し、
且つ貴重な資源として回収でき、凝集汚泥及び余剰汚泥
の発生量を大きく減少させ、更に無機凝集剤の使用量も
削減できる。本発明において、リン、アンモニアを含む
有機性汚水を生物処理する工程に、水酸化鉄微粒子、ゼ
オライト微粒子を添加してリン、アンモニア分を除去
し、且つ回収することで、該汚水中のリンを有効に除去
し、且つリン資源として回収できる。また、活性汚泥か
らリンを溶出させる工程で汚泥の量が減少すため、余剰
生物汚泥の発生量及び凝集汚泥の発生量が減少するの
で、汚泥処理が著しく合理化される。水酸化鉄、ゼオラ
イトは吸着剤として再利用できるため、水酸化鉄、ゼオ
ライトに使用量が少なくてすむ。さらにアンモニア分の
除去に反応速度の遅い生物学的硝化脱窒素法を適用する
必要がなく、ゼオライト微粒子が活性汚泥の沈降促進剤
として機能する。曝気槽のＭＬＶＳＳを高くできるので
生物処理を高速で行なえる。According to the present invention, in the method for treating organic wastewater, phosphorus and ammonia are removed from the organic wastewater,
In addition, it can be recovered as a valuable resource, greatly reducing the amount of coagulated sludge and excess sludge generated, and further reducing the amount of inorganic coagulant used. In the present invention, phosphorus and fine particles of zeolite are added to the step of biologically treating organic wastewater containing phosphorus and ammonia to remove phosphorus and ammonia, and to recover phosphorus in the wastewater. It can be effectively removed and recovered as phosphorus resources. In addition, since the amount of sludge is reduced in the step of eluting phosphorus from activated sludge, the amount of surplus biological sludge and the amount of coagulated sludge are reduced, so that sludge treatment is significantly streamlined. Since iron hydroxide and zeolite can be reused as an adsorbent, a small amount of iron hydroxide and zeolite can be used. Further, there is no need to apply a biological nitrification denitrification method having a slow reaction rate to remove the ammonia content, and the zeolite fine particles function as a sedimentation accelerator for activated sludge. Since the MLVSS in the aeration tank can be increased, biological treatment can be performed at high speed.
【図１】本発明の実施の態様の一例を示す概念図であ
る。FIG. 1 is a conceptual diagram showing an example of an embodiment of the present invention.
１ 曝気槽 ２ 沈殿槽 ３ 脱着槽 ４ 固液分離部 ５ ＭＡＰ生成槽 ６ 固液分離部 １１ 有機性汚水 １２ 水酸化鉄、ゼオライト微粒子 １３ 処理水 １４ 沈殿汚泥 １５ 返送汚泥 １６ 回収汚泥 １７ アルカリ １８ 分離液 １９ 分離汚泥 ２０ マグネシウム化合物 ２１ 回収ＭＡＰ ２２ 分離液 REFERENCE SIGNS LIST 1 aeration tank 2 sedimentation tank 3 desorption tank 4 solid-liquid separation unit 5 MAP generation tank 6 solid-liquid separation unit 11 organic wastewater 12 iron hydroxide, zeolite fine particles 13 treated water 14 settled sludge 15 return sludge 16 recovered sludge 17 alkali 18 separation Liquid 19 Separated sludge 20 Magnesium compound 21 Recovered MAP 22 Separated liquid
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D028 AA08 AC01 BB06 BC28 BD11 BD16 BE01 BE04 BE08 4D038 AA08 AB28 AB29 AB43 BA02 BA04 BB06 BB13 BB18 BB19 BB20 4D059 AA06 AA19 BE00 BE53 BF02 BF14 CA24 CA28 CC01 DA08 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D028 AA08 AC01 BB06 BC28 BD11 BD16 BE01 BE04 BE08 4D038 AA08 AB28 AB29 AB43 BA02 BA04 BB06 BB13 BB18 BB19 BB20 4D059 AA06 AA19 BE00 BE53 BF02 BF14 CA24 CA28 CC08 DA08
Claims (2)
物処理する際に、水酸化鉄、ゼオライトを共存させて、
リン、アンモニアを吸着除去する生物処理工程Ａと、生
物処理工程Ａの活性汚泥の一部を引抜いてアルカリ剤を
添加し、該活性汚泥からリン、アンモニアを溶出させ、
且つ該活性汚泥を可溶化し、その後固液分離する工程Ｂ
と、該固液分離からの分離液にマグネシウム化合物を添
加してリン及びアンモニアをリン酸マグネシウムアンモ
ニウムとして回収する工程Ｃを有することを特徴とする
有機性汚水の処理方法。When biological treatment of organic wastewater containing phosphorus and ammonia, iron hydroxide and zeolite coexist,
Biological treatment step A for adsorbing and removing phosphorus and ammonia, a part of the activated sludge of biological treatment step A is withdrawn and an alkaline agent is added, and phosphorus and ammonia are eluted from the activated sludge,
And a step B of solubilizing the activated sludge and thereafter performing solid-liquid separation.
And a step C of adding a magnesium compound to the separated liquid from the solid-liquid separation to recover phosphorus and ammonia as magnesium ammonium phosphate.
泥を共存する水酸化鉄、ゼオライトとともに、前記生物
処理工程Ａに供給することを特徴とする請求項１記載の
有機性汚水の処理方法。2. The organic wastewater treatment according to claim 1, wherein the separated sludge obtained by the solid-liquid separation in the step B is supplied to the biological treatment step A together with coexisting iron hydroxide and zeolite. Method.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11118270A JP2000308895A (en) | 1999-04-26 | 1999-04-26 | Treatment of organic sewage |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11118270A JP2000308895A (en) | 1999-04-26 | 1999-04-26 | Treatment of organic sewage |
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| Publication Number | Publication Date |
|---|---|
| JP2000308895A true JP2000308895A (en) | 2000-11-07 |
Family
ID=14732494
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|---|---|---|---|
| JP11118270A Withdrawn JP2000308895A (en) | 1999-04-26 | 1999-04-26 | Treatment of organic sewage |
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|---|---|
| JP (1) | JP2000308895A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002263676A (en) * | 2001-03-09 | 2002-09-17 | Sumitomo Heavy Ind Ltd | Waste water treatment method and facility |
| CN102639450A (en) * | 2009-07-08 | 2012-08-15 | 沙特阿拉伯石油公司 | Low concentration wastewater treatment system and process |
| US9290399B2 (en) | 2009-07-08 | 2016-03-22 | Saudi Arabian Oil Company | Wastewater treatment process including irradiation of primary solids |
| CN111186971A (en) * | 2020-01-08 | 2020-05-22 | 上海海洋大学 | Recoverable bottom mud covering device and application |
-
1999
- 1999-04-26 JP JP11118270A patent/JP2000308895A/en not_active Withdrawn
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002263676A (en) * | 2001-03-09 | 2002-09-17 | Sumitomo Heavy Ind Ltd | Waste water treatment method and facility |
| JP4680403B2 (en) * | 2001-03-09 | 2011-05-11 | 住友重機械エンバイロメント株式会社 | Wastewater treatment method and apparatus |
| CN102639450A (en) * | 2009-07-08 | 2012-08-15 | 沙特阿拉伯石油公司 | Low concentration wastewater treatment system and process |
| CN104386816A (en) * | 2009-07-08 | 2015-03-04 | 沙特阿拉伯石油公司 | Low concentration wastewater treatment system and process |
| CN102639450B (en) * | 2009-07-08 | 2015-06-03 | 沙特阿拉伯石油公司 | Low concentration wastewater treatment system and process |
| US9073764B2 (en) | 2009-07-08 | 2015-07-07 | Saudi Arabian Oil Company | Low concentration wastewater treatment system and process |
| US9290399B2 (en) | 2009-07-08 | 2016-03-22 | Saudi Arabian Oil Company | Wastewater treatment process including irradiation of primary solids |
| US9340441B2 (en) | 2009-07-08 | 2016-05-17 | Saudi Arabian Oil Company | Wastewater treatment system including irradiation of primary solids |
| CN111186971A (en) * | 2020-01-08 | 2020-05-22 | 上海海洋大学 | Recoverable bottom mud covering device and application |
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