JPH08141592A - Anaerobic treatment method - Google Patents
Anaerobic treatment methodInfo
- Publication number
- JPH08141592A JPH08141592A JP29129794A JP29129794A JPH08141592A JP H08141592 A JPH08141592 A JP H08141592A JP 29129794 A JP29129794 A JP 29129794A JP 29129794 A JP29129794 A JP 29129794A JP H08141592 A JPH08141592 A JP H08141592A
- Authority
- JP
- Japan
- Prior art keywords
- water
- tank
- acid
- uasb
- reaction tank
- 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.)
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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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は嫌気性処理法に係り、特
に、焼酎廃液、ウイスキー蒸留廃液、ビール仕込排水な
どの、窒素及びリンの栄養塩類を含む高濃度有機性排水
をＵＡＳＢ嫌気処理で効率的に処理して、有機物と共
に、窒素及びリンの同時除去も可能とする嫌気性処理法
に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an anaerobic treatment method, and more particularly, to UASB anaerobic treatment of high-concentration organic wastewater containing nutrient salts of nitrogen and phosphorus, such as shochu liquor, whiskey distillation effluent, and beer-charged wastewater. The present invention relates to an anaerobic treatment method capable of efficiently treating and simultaneously removing nitrogen and phosphorus together with organic substances.
【０００２】[0002]
【従来の技術】ＵＡＳＢ法、即ち、上向流嫌気性汚泥床
法（Upflow Anaerobic Sludge Blanket Process)は、嫌
気性菌（メタン生成細菌）を、付着担体を用いることな
く自己造粒又は核となる物質に造粒させてなる造粒汚泥
（グラニュール）の汚泥床（スラッジブランケット）を
形成した反応槽（ＵＡＳＢ型メタン生成槽）に、原水を
上向流で通水して処理する方法であり、反応槽中に高濃
度の微生物を保持することが可能であることから、高負
荷処理にて、有機性排水中の有機物を効率良く分解除去
することができる方法である。ＵＡＳＢ法は、好気性活
性汚泥法に比べて、反応槽容積当りの有機物負荷が１０
ｋｇ−ＣＯＤcr／ｍ3 ／ｄａｙ以上と高く、曝気のため
のエネルギーが不要で、メタンガスとしてエネルギーの
回収が可能である上に、余剰汚泥発生量が少ないといっ
た優れた特長を備えている。2. Description of the Related Art The UASB method, that is, the Upflow Anaerobic Sludge Blanket Process, makes anaerobic bacteria (methanogenic bacteria) self-granulate or nucleate without using an adherent carrier. It is a method in which raw water is passed through an upward flow to a reaction tank (UASB-type methane production tank) in which a sludge bed (sludge blanket) of granulated sludge (granule) formed by granulating substances is formed. Since it is possible to retain a high concentration of microorganisms in the reaction tank, it is a method capable of efficiently decomposing and removing the organic matter in the organic waste water by high-load treatment. Compared with the aerobic activated sludge method, the UASB method has an organic matter load of 10 per volume of the reaction tank.
It has a high value of kg-COD cr / m 3 / day or more, does not require energy for aeration, can recover energy as methane gas, and has an excellent feature that the amount of excess sludge generated is small.
【０００３】一方、アンモニア性窒素及び正リン酸が共
存する系内に、マグネシウム塩が存在すると、アルカリ
性条件ではＭｇＮＨ4 ＰＯ4 ・６Ｈ2 Ｏ（リン酸アンモ
ニウムマグネシウム（ＭＡＰ））の結晶が生成すること
は良く知られている。この反応は、通常、アルカリ側で
ＮＨ4 −Ｎ＞１００ｍｇ／ｌの条件で進行すると言われ
ている。On the other hand, when a magnesium salt is present in the system in which ammoniacal nitrogen and orthophosphoric acid coexist, MgNH 4 PO 4 .6H 2 O (magnesium ammonium phosphate (MAP)) crystals are formed under alkaline conditions. It is well known. It is said that this reaction usually proceeds on the alkaline side under the condition of NH 4 —N> 100 mg / l.
【０００４】[0004]
【発明が解決しようとする課題】ＵＡＳＢ法において、
余剰汚泥発生量が少ないという特長は、逆に、排水中の
栄養塩類を菌体中に取り込む量が少ないということを意
味し、このため、ＵＡＳＢ法では、原水中に含まれる窒
素やリンが、菌体に同化されて除去されるという効果は
期待できない。このようなことから、ＵＡＳＢ法による
処理のみで、有機物と共に窒素やリンを除去することは
困難であり、閉鎖性水域の富栄養化現象となる窒素やリ
ンを除去するためには、硝化／脱窒や凝集沈澱などの後
処理プロセスを組み合わせる必要がある。DISCLOSURE OF THE INVENTION In the UASB method,
On the contrary, the feature that the amount of excess sludge generated is small means that the amount of nutrient salts in the wastewater taken into the bacterial cells is small. Therefore, in the UASB method, nitrogen and phosphorus contained in the raw water are The effect of being assimilated by bacterial cells and removed cannot be expected. From this, it is difficult to remove nitrogen and phosphorus together with organic matter only by the treatment by the UASB method, and in order to remove nitrogen and phosphorus which are eutrophication phenomena in closed water areas, nitrification / denitration is required. It is necessary to combine post-treatment processes such as nitrification and coagulation precipitation.
【０００５】ところで、ＵＡＳＢ法の操作上の問題点と
して、グラニュール汚泥の浮上、流出が挙げられる。グ
ラニュール汚泥の浮上、流出は、処理水質の悪化とＵＡ
ＳＢ反応槽内の菌体量の減少をもたらすため、これを防
止する技術が求められている。By the way, as a problem in the operation of the UASB method, floating and outflow of granule sludge can be mentioned. Floating and outflow of granule sludge causes deterioration of treated water quality and UA.
Since the amount of bacterial cells in the SB reaction tank is reduced, a technique for preventing this is required.
【０００６】前記ＭＡＰの生成反応を、ＵＡＳＢ反応槽
内で生起させ、グラニュール汚泥中にＭＡＰを析出させ
ることができるならば、ＵＡＳＢ法による有機物と窒素
及びリンの同時除去が可能となる上に、汚泥中の無機分
が相対的に増加するため汚泥の沈降性を向上させること
ができる。[0006] If the MAP formation reaction can be caused to occur in the UASB reaction tank and MAP can be precipitated in the granulated sludge, the organic substances and nitrogen and phosphorus can be simultaneously removed by the UASB method. Since the inorganic content in the sludge relatively increases, the sedimentation property of the sludge can be improved.
【０００７】このようなことから、ｐＨをアルカリ側と
すると共に、マグネシウム塩を添加した原水をＵＡＳＢ
法により嫌気性処理することも検討されているが、この
場合には、ＭＡＰの結晶はグラニュール汚泥中のみなら
ず、流速の大きい配管内やポンプ内にもスケールとなっ
て析出し、配管閉塞、ポンプの作動不良などの問題を引
き起こす。特に、ＵＡＳＢ反応槽内部にまで延びる原水
供給配管にスケールが付着した場合には、スケール除去
は極めて困難である。From the above, the pH is set to the alkaline side and the raw water containing magnesium salt is added to the UASB.
Although anaerobic treatment by the method is also considered, in this case, MAP crystals are deposited not only in the granulated sludge but also in the pipe with a high flow rate and in the pump as a scale, resulting in blockage of the pipe. , Causing problems such as pump malfunction. Particularly, when the scale adheres to the raw water supply pipe extending to the inside of the UASB reaction tank, it is extremely difficult to remove the scale.
【０００８】しかも、水中に生成したＭＡＰ粒子は、処
理水中に浮遊して流出するため、除去効果は十分である
とはいえない。Moreover, the MAP particles produced in water are suspended in the treated water and flow out, so that it cannot be said that the removal effect is sufficient.
【０００９】本発明は上記従来の問題点を解決し、スケ
ーリングを引き起こすことなく、グラニュール汚泥表面
又は汚泥内のみにＭＡＰを析出させることにより、ＵＡ
ＳＢ法により有機物と窒素及びリンの同時除去を行うと
共に、グラニュール汚泥の浮上、流出を防止する嫌気性
処理法を提供することを目的とする。The present invention solves the above-mentioned conventional problems and allows UA to be deposited only on the surface of or within granule sludge without causing scaling.
It is an object of the present invention to provide an anaerobic treatment method for simultaneously removing organic matters, nitrogen and phosphorus by the SB method and preventing floating and outflow of granule sludge.
【００１０】[0010]
【課題を解決するための手段】本発明の嫌気性処理法
は、窒素及びリンを含有する有機性排水を酸生成槽で処
理した後、ＵＡＳＢ型メタン生成槽で処理する方法にお
いて、酸生成槽の流入水又は流出水にマグネシウム塩を
添加すると共に、ＵＡＳＢ型メタン生成槽の流入水のｐ
Ｈを５．８〜６．５に調整することを特徴とする。The anaerobic treatment method of the present invention is a method of treating organic wastewater containing nitrogen and phosphorus in an acid generation tank and then in a UASB type methane generation tank. In addition to adding magnesium salt to the inflow water or outflow water of the
It is characterized in that H is adjusted to 5.8 to 6.5.
【００１１】以下、図面を参照して本発明の嫌気性処理
法を詳細に説明する。The anaerobic treatment method of the present invention will be described in detail below with reference to the drawings.
【００１２】図１は本発明の嫌気性処理法の一実施例方
法を説明する系統図である。FIG. 1 is a system diagram for explaining a method of an embodiment of the anaerobic treatment method of the present invention.
【００１３】図１に示す方法において、焼酎廃水、ウイ
スキー蒸留廃水、ビール仕込排水などの原水を、配管１
１よりまず酸生成槽１に導入し、水中の糖、タンパクな
どを、乳酸、プロピオン酸、ラク酸、酢酸などの揮発性
低級脂肪酸に分解する。即ち、酸生成槽１では、酸生成
細菌が浮遊状態で又は担体に固定された状態で存在して
おり、低級脂肪酸への分解反応が行われる。In the method shown in FIG. 1, raw water such as shochu wastewater, whiskey distilling wastewater, beer preparation wastewater, etc. is supplied to the pipe 1
First, it is introduced into the acid generation tank 1 from 1, and sugars, proteins and the like in water are decomposed into volatile lower fatty acids such as lactic acid, propionic acid, lactic acid and acetic acid. That is, in the acid production tank 1, the acid production bacteria exist in a floating state or in a state of being fixed to a carrier, and a decomposition reaction into lower fatty acids is performed.
【００１４】本実施例においては、この酸生成槽１に、
後段のＵＡＳＢ反応槽２の処理水の一部を配管１２，１
３より循環すると共に、マグネシウム（Ｍｇ）塩を配管
１４より添加する。In this embodiment, the acid production tank 1 is
A part of the treated water in the latter-stage UASB reaction tank 2 is piped 12,
While circulating from No. 3, magnesium (Mg) salt is added from the pipe 14.
【００１５】このように、ＵＡＳＢ反応槽２の処理水の
一部を循環することにより、酸生成槽１における酸生成
による極端なｐＨ低下を防止して、酸生成速度を高める
と共に、後述のＵＡＳＢ反応槽２の流入水のｐＨ調整の
ためのアルカリ添加量の低減を図ることができる。By circulating a portion of the treated water in the UASB reaction tank 2 in this manner, an extreme decrease in pH due to acid generation in the acid generation tank 1 is prevented, the acid generation rate is increased, and the UASB described later is used. It is possible to reduce the amount of alkali added for adjusting the pH of the inflow water of the reaction tank 2.
【００１６】この酸生成槽１内は処理水の循環水量や原
水濃度等によっても異なるが、通常ｐＨが４〜６．５の
弱酸性状態になっており、この中でのＭＡＰの析出はな
い。酸生成槽１には必要に応じて、アルカリを添加する
こともできるが、ｐＨはあくまでも上記範囲とするのが
好ましい。The inside of the acid production tank 1 is usually in a weakly acidic state of pH 4 to 6.5, though it varies depending on the circulating water amount of the treated water, the concentration of raw water, etc., and there is no deposition of MAP therein. . If necessary, an alkali may be added to the acid production tank 1, but the pH is preferably kept within the above range.
【００１７】酸生成槽１に添加するＭｇ塩としては、水
酸化マグネシウム（Ｍｇ（ＯＨ）2）、酸化マグネシウ
ム（ＭｇＯ）、塩化マグネシウム（ＭｇＣｌ2 ）、硫酸
マグネシウム（ＭｇＳＯ4 ）等を用いることができ、こ
れらのうち、アルカリ剤としてｐＨ調整にも有効である
ことからＭｇ（ＯＨ）2 を用いるのが好ましい。なお、
系内のｐＨが６．５を超えるような場合には、ＭｇＣｌ
2 等の酸性塩を添加する。As the Mg salt added to the acid generator 1, magnesium hydroxide (Mg (OH) 2 ), magnesium oxide (MgO), magnesium chloride (MgCl 2 ), magnesium sulfate (MgSO 4 ), etc. may be used. Of these, Mg (OH) 2 is preferably used because it is effective as an alkaline agent for pH adjustment. In addition,
If the pH in the system exceeds 6.5, MgCl 2
Add an acid salt such as 2 .
【００１８】Ｍｇ塩の添加割合は、除去すべきリン、即
ち、原水中のリンの１モル倍以上、好ましくは１．１〜
１．５モル倍とする。The addition ratio of the Mg salt is 1 mol times or more of the phosphorus to be removed, that is, phosphorus in the raw water, preferably 1.1 to.
1.5 mol times.
【００１９】酸生成槽１の流出水は、次いで、配管１５
よりＵＡＳＢ反応槽２に送給されるが、この過程で配管
１６より必要に応じて水酸化ナトリウム（ＮａＯＨ）等
のアルカリが添加されて、ｐＨ５．８〜６．５の範囲に
調整される。１７はｐＨ計である。The outflow water of the acid production tank 1 is then supplied to the pipe 15
Although it is fed to the UASB reaction tank 2, an alkali such as sodium hydroxide (NaOH) is added from the pipe 16 as needed in this process to adjust the pH to the range of 5.8 to 6.5. 17 is a pH meter.
【００２０】この調整ｐＨが５．８未満では生物活性が
低下し、ＵＡＳＢ反応槽２内でのメタン生成効率が低下
する。逆に、調整ｐＨが６．５を超えるとこの配管１５
内でＭＡＰの析出が起こり、スケール生成により配管閉
塞を引き起こしたり、ＵＡＳＢ反応槽２内において、後
述の如く、グラニュール汚泥の表面や内部でのＭＡＰの
析出のみならず、液中でもＭＡＰが析出することによ
り、処理水中にＭＡＰが流出したりするなどの不具合が
生じる。When the adjusted pH is less than 5.8, the biological activity is lowered and the efficiency of methane production in the UASB reaction tank 2 is lowered. Conversely, if the adjusted pH exceeds 6.5, this pipe 15
Precipitation of MAP occurs in the interior, causing pipe clogging due to scale formation, and in the UASB reaction tank 2, not only precipitation of MAP on the surface and inside of the granulated sludge as described later, but also MAP precipitates in the liquid This causes a problem such as MAP flowing out into the treated water.
【００２１】ＵＡＳＢ反応槽２に流入した酸生成処理水
は、Ｍｇ塩を含有すると共に、そのｐＨが５．８〜６．
５の範囲に調整されたものであるが、ＵＡＳＢ反応槽２
内で嫌気性処理され、有機酸からのメタン生成の進行に
伴ってｐＨが上昇し、例えば、焼酎廃液やウイスキー蒸
留廃液では通常の場合ｐＨ７．５〜８となる。このｐＨ
の上昇に伴って、系内のＰＯ4 −Ｐ，ＮＨ4 −Ｎ，Ｍｇ
2+が反応し、グラニュール汚泥表面やグラニュール汚泥
内部にＭＡＰが析出する。The acid-forming treated water that has flowed into the UASB reactor 2 contains Mg salt and has a pH of 5.8 to 6.
Although adjusted to the range of 5, the UASB reaction tank 2
It is anaerobically treated and the pH increases with the progress of methane production from organic acids. For example, in the case of shochu waste liquid and whiskey distillation waste liquid, the pH is usually 7.5 to 8. This pH
With increasing temperature, PO 4 -P, NH 4 -N, Mg in the system
2+ reacts and MAP is deposited on the surface of the granulated sludge and inside the granulated sludge.
【００２２】これにより、メタン生成反応による有機物
の分解と共に、ＵＡＳＢ反応槽２内のグラニュール汚泥
内に、原水中のリン及び窒素が固定化され、有機物、リ
ン及び窒素が除去された処理水は、その一部が配管１
２，１３より酸生成槽１に循環され、残部は配管１８よ
り系外へ排出される。As a result, phosphorus and nitrogen in the raw water are fixed in the granulated sludge in the UASB reaction tank 2 along with the decomposition of organic matter by the methane production reaction, and the treated water from which organic matter, phosphorus and nitrogen have been removed is treated. , Part of which is piping 1
It is circulated to the acid production tank 1 from Nos. 2 and 13, and the rest is discharged from the system through the pipe 18.
【００２３】なお、生成したＭＡＰ含有グラニュール汚
泥は、ＭＡＰ析出により比重が増大することにより、沈
降性が高くなり、ＵＡＳＢ反応槽内での浮上及びＵＡＳ
Ｂ反応槽からの流出が防止される。余剰汚泥は、配管１
９より抜き出し、従来と同様に脱水埋立処分することが
可能であるが、乾燥させた後に肥料として有効利用する
ことも可能である。The MAP-containing granulated sludge thus produced has a higher specific gravity due to the increased MAP precipitation, and thus has a higher sedimentation property, and is floated in the UASB reaction tank and UASB.
Outflow from the B reactor is prevented. Excess sludge is pipe 1
Although it can be extracted from No. 9 and disposed of in a dehydrated landfill as in the conventional case, it can also be effectively used as fertilizer after being dried.
【００２４】図１に示す方法は、本発明の一実施例方法
を示すものであって、本発明はその要旨を超えない限
り、何ら図示の方法に限定されるものではない。The method shown in FIG. 1 shows an embodiment method of the present invention, and the present invention is not limited to the illustrated method as long as the gist thereof is not exceeded.
【００２５】例えば、ＵＡＳＢ反応槽２の処理水の一部
を循環する場合、この循環はｐＨ調整のためのアルカリ
添加量の低減のために行うものであるから、図１に示す
如く、酸生成槽１に循環するものに限られず、酸生成槽
の流出水、即ち、配管１２，２０を経て、配管１５内に
注入しても良い。また、原水の導入配管１１に注入する
ことも可能であり、いずれの場合も同様の効果を得るこ
とができる。For example, when a portion of the treated water in the UASB reaction tank 2 is circulated, this circulation is carried out to reduce the amount of alkali added for pH adjustment. Therefore, as shown in FIG. The water is not limited to the one circulating in the tank 1, and may be injected into the pipe 15 through the water flowing out of the acid generation tank, that is, the pipes 12 and 20. Further, it is also possible to inject the raw water into the introduction pipe 11, and in any case, the same effect can be obtained.
【００２６】また、Ｍｇ塩の添加についても、酸生成槽
１に添加する他、原水導入配管１１、酸生成槽の流出水
配管１５に添加しても良い。Regarding addition of the Mg salt, in addition to the addition to the acid production tank 1, it may be added to the raw water introduction pipe 11 and the outflow water pipe 15 of the acid production tank.
【００２７】なお、本発明の方法においては、生物反応
とＭＡＰの析出による窒素及びリンの除去を共存させる
必要上、生物の増殖量とＭＡＰ生成量をある程度の範囲
でバランスさせる必要がある。例えば、生成するＭＡＰ
が生物増殖量よりもはるかに多ければ、微生物のＳＲＴ
が維持できなくなり、生物処理が不可能となる。従っ
て、この生物反応とＭＡＰの生成とのバランスの面か
ら、本発明の方法は、実用的には、ＣＯＤcr濃度に対し
て２％程度以下のＴ−Ｐ濃度の原水に適用するのが有効
である。In the method of the present invention, the biological reaction and the removal of nitrogen and phosphorus by the precipitation of MAP need to be coexistent, and the growth amount of the organism and the MAP production amount must be balanced to some extent. For example, MAP to generate
Is much higher than the amount of organism growth, SRT of microorganisms
Can no longer be maintained, making biological treatment impossible. Therefore, from the viewpoint of the balance between this biological reaction and the formation of MAP, it is effective that the method of the present invention is practically applied to raw water having a T-P concentration of about 2% or less with respect to the COD cr concentration. Is.
【００２８】[0028]
【作用】本発明において、ＵＡＳＢ反応槽には、Ｍｇ塩
を含有すると共にｐＨが５．８〜６．５の被処理水が導
入される。In the present invention, the water to be treated containing Mg salt and having a pH of 5.8 to 6.5 is introduced into the UASB reactor.
【００２９】この被処理水はＭｇ塩を含有するが、その
ｐＨが５．８〜６．５であり、ＭＡＰが生成するｐＨ条
件より低ｐＨであるため、ＵＡＳＢ反応槽への被処理水
導入配管等にＭＡＰの析出は殆どみられない。しかし、
ＵＡＳＢ反応槽内では有機酸からメタンが生成すること
によりｐＨが上昇する。このｐＨの変化はＵＡＳＢ反応
槽の入口から出口側へ向って徐々に上昇するものではな
く、ＵＡＳＢ反応槽内は発生するメタンガスによる攪乱
で完全混合状態に近い状態となっているため、被処理水
の導入配管からＵＡＳＢ反応槽内に流入した瞬間にｐＨ
上昇が起こる。This water to be treated contains Mg salt, but its pH is 5.8 to 6.5, which is lower than the pH condition for producing MAP, so that the water to be treated is introduced into the UASB reactor. Almost no deposition of MAP was found in the piping. But,
In the UASB reaction tank, the pH rises due to the production of methane from the organic acid. This change in pH does not gradually increase from the inlet to the outlet of the UASB reaction tank, and the inside of the UASB reaction tank is in a state close to a completely mixed state due to the disturbance by the generated methane gas. PH at the moment when it flows into the UASB reaction tank from the introduction pipe of
A rise occurs.
【００３０】このｐＨ上昇により、ＵＡＳＢ反応槽系内
は一般にＭＡＰ析出条件のアルカリ側となっており、被
処理水中のリン、窒素及びＭｇ塩がこのＭＡＰ析出ｐＨ
条件下で反応してグラニュール汚泥表面にＭＡＰが析出
する。グラニュール汚泥はその表面、即ち、液との界面
よりも、内部でより高ｐＨ条件となっているため、ＭＡ
Ｐの析出はグラニュール汚泥内部でも起こる。Due to this increase in pH, the inside of the UASB reaction tank system is generally on the alkaline side of the MAP precipitation conditions, and the phosphorus, nitrogen and Mg salts in the water to be treated are the MAP precipitation pH.
MAP is deposited on the surface of the granulated sludge by reacting under the conditions. Granule sludge has a higher pH condition on the inside than on the surface, that is, the interface with the liquid, so
Precipitation of P also occurs inside the granulated sludge.
【００３１】このため、本発明の方法によれば、ＵＡＳ
Ｂ反応槽内において、有機物の分解除去と共に、リン及
び窒素をＭＡＰの形で除去してグラニュール汚泥内に固
定化することができる。Therefore, according to the method of the present invention, the UAS
In the B reaction tank, phosphorus and nitrogen can be removed in the form of MAP along with decomposition and removal of organic matter, and immobilized in the granule sludge.
【００３２】しかして、ＭＡＰを含有するグラニュール
汚泥は、無機分が相対的に増加することによりその比重
が増大し、このため沈降性が著しく高められる。これに
より、ＵＡＳＢ反応槽内でのグラニュール汚泥の浮上及
びＵＡＳＢ反応槽からのグラニュール汚泥の流出が防止
され、汚泥の流出による処理水の悪化を防止すると共
に、ＵＡＳＢ反応槽内の菌体量を高く維持して高負荷処
理を行うことが可能となる。However, the specific gravity of the MAP-containing granule sludge increases due to the relative increase in the inorganic content, and therefore the sedimentation property is significantly enhanced. As a result, the floating of granule sludge in the UASB reaction tank and the outflow of granule sludge from the UASB reaction tank are prevented, the deterioration of treated water due to the outflow of sludge is prevented, and the amount of bacterial cells in the UASB reaction tank is prevented. It is possible to maintain a high value and perform high load processing.
【００３３】因みに、ＵＡＳＢ反応槽流入水の調整ｐＨ
が５．８未満であると、ｐＨ値が低過ぎて生物活性が低
下し、ＵＡＳＢ反応槽における反応効率が悪く、メタン
生成量、即ち、有機酸分解量が低減する。Incidentally, the adjusted pH of the inflow water of the UASB reaction tank
Is less than 5.8, the pH value is too low, the biological activity is lowered, the reaction efficiency in the UASB reaction tank is poor, and the methane production amount, that is, the organic acid decomposition amount is reduced.
【００３４】逆に、ＵＡＳＢ反応槽流入水の調整ｐＨが
６．５以上、特に７以上では、流入水配管中やＵＡＳＢ
反応槽内の液中でのＭＡＰ析出が起こるようになる。こ
の場合には、配管内にスケールが生成して配管閉塞を引
き起こす。また、ＵＡＳＢ反応槽の液中で生成したコロ
イダルＭＡＰがグラニュール汚泥内に取り込まれること
なくそのまま処理水中に流出し、処理水水質が悪化する
などの問題が生じる。On the contrary, when the adjusted pH of the inflow water of the UASB reaction tank is 6.5 or more, particularly 7 or more, the inflow water pipe or the UASB is
Precipitation of MAP occurs in the liquid in the reaction tank. In this case, scale is generated in the pipe and causes pipe clogging. Further, the colloidal MAP produced in the liquid in the UASB reaction tank flows out into the treated water as it is without being taken into the granulated sludge, which causes a problem that the quality of the treated water deteriorates.
【００３５】[0035]
【実施例】以下に実施例及び比較例を挙げて本発明をよ
り具体的に説明する。EXAMPLES The present invention will be described more specifically with reference to Examples and Comparative Examples below.
【００３６】実施例１，２、比較例１，２ 図１に示す方法に従って、下記基質を含む下記水質の原
水の処理を行った。Examples 1, 2 and Comparative Examples 1, 2 Raw water of the following water quality containing the following substrates was treated according to the method shown in FIG.
【００３７】原水（ｍｇ／ｌ） グルコース： １５０００ エタノール： ５０００ 酵母エキス： ６００ ＮＨ4 −Ｎ： ４００ ＰＯ4 −Ｐ： １５０ ＣＯＤcr ：約２２０００ 酸生成槽及びＵＡＳＢ反応槽の仕様並びに処理条件は下
記の通りとし、酸生成槽にＭｇ塩としてＭｇＣｌ2 ・２
Ｈ2 Ｏを３６５ｍｇ／ｌ（Ｍｇ／Ｐ＝１．３モル比）添
加すると共に、酸生成槽の流出液にＮａＯＨを添加し
て、表１に示すｐＨ条件に調整した。 Raw water (mg / l) Glucose: 15000 Ethanol: 5000 Yeast extract: 600 NH 4 -N: 400 PO 4 -P: 150 COD cr : about 22000 The specifications and treatment conditions of the acid production tank and the UASB reaction tank are as follows. And MgCl 2 · 2 as Mg salt in the acid generation tank.
H 2 O was added at 365 mg / l (Mg / P = 1.3 molar ratio), and NaOH was added to the effluent of the acid generator to adjust the pH conditions shown in Table 1.
【００３８】処理条件等 酸生成槽：容量２．５リットル（直径１０ｃｍ×高さ３
２ｃｍ） ＵＡＳＢ反応槽：容量９リットル（直径１０ｃｍ×高さ
１．２ｍ） 温度：３０℃（３０℃の恒温室内にて実施） 通液量：６．０〜６．２リットル／日 ＣＯＤcr負荷：１４．３〜１５．１ｋｇ−ＣＯＤcr／ｍ
3 ／日 処理水循環量：原水量の１０倍（酸生成槽のみに循環） 各々、２週間処理を継続して行い、ＵＡＳＢ反応槽にお
ける発生メタンガス量を測定すると共に、処理水水質を
調べてＳ−ＣＯＤcr、Ｔ−Ｐ及びＮＨ4 −Ｈの除去率を
求め、２週間の平均結果を表１に示した。 Treatment conditions, etc. Acid generating tank: capacity 2.5 liters (diameter 10 cm x height 3
2 cm) UASB reaction tank: Capacity 9 liters (diameter 10 cm x height 1.2 m) Temperature: 30 ° C (conducted in a constant temperature room at 30 ° C) Liquid flow rate: 6.0 to 6.2 liters / day COD cr load : 14.3 to 15.1 kg-COD cr / m
3 / day Circulation amount of treated water: 10 times the amount of raw water (circulation only in the acid production tank) Each treatment was continued for 2 weeks, the amount of methane gas generated in the UASB reaction tank was measured, and the quality of the treated water was investigated. The removal rates of —COD cr , T-P and NH 4 —H were determined, and the average results for 2 weeks are shown in Table 1.
【００３９】また、ＵＡＳＢ反応槽の流入配管内部にス
テンレス（ＳＵＳ３０４）テストピースを浸漬させ、付
着したスケール量を測定し、結果を表１に示した。Further, a stainless (SUS304) test piece was dipped inside the inflow pipe of the UASB reaction tank, and the amount of attached scale was measured. The results are shown in Table 1.
【００４０】[0040]
【表１】 [Table 1]
【００４１】表１より次のことが明らかである。The following is clear from Table 1.
【００４２】即ち、比較例１では、ＵＡＳＢ反応槽の流
入水のｐＨがやや低いことから有機物処理が不安定であ
り、プロピオン酸、酢酸を中心に残留ＣＯＤcrが高く、
ＵＡＳＢ反応槽内ｐＨも６．６程度のため、処理水の窒
素、リン濃度は原水と殆ど変わらない。実施例１，２で
は、いずれも、メタン生成も良好であり、良好な処理が
行われている。因みに、処理水中の溶解性ＣＯＤcrは１
０００ｍｇ／ｌ以下であった。また、窒素、リンの除去
率も７０％程度と良好であった。比較例２でも、ほぼ同
様にメタン生成は良好に進行していたが、微細なコロイ
ダルＭＡＰの生成によって処理水のＴ−Ｐ濃度は、実施
例１，２と比較してやや高かった。また、テストピース
表面に付着したスケールは、１ｃｍ2 当りで比較する
と、比較例２が圧倒的に大きく、長期間の運転では配管
閉塞が予想される。That is, in Comparative Example 1, since the pH of the inflow water of the UASB reaction tank was slightly low, the treatment of organic substances was unstable, and the residual COD cr was high mainly in propionic acid and acetic acid.
Since the pH in the UASB reaction tank is about 6.6, the nitrogen and phosphorus concentrations of the treated water are almost the same as the raw water. In each of Examples 1 and 2, methane production was good, and good treatment was performed. By the way, the soluble COD cr in the treated water is 1
It was 000 mg / l or less. In addition, the removal rate of nitrogen and phosphorus was good at about 70%. In Comparative Example 2 as well, methane production proceeded satisfactorily almost similarly, but the TP concentration of the treated water was slightly higher than in Examples 1 and 2 due to the production of fine colloidal MAP. In addition, the scale attached to the surface of the test piece is overwhelmingly large in Comparative Example 2 when compared per 1 cm 2 , and pipe clogging is expected in long-term operation.
【００４３】なお、実施例１において、ｐＨ調整に必要
なＮａＯＨ量は３４ｇ−ＮａＯＨ／ｋｇ−ＣＯＤcrであ
った。一方、処理水を図１に示す配管１２，２０を経て
酸生成槽の流出水配管（配管１５）に循環した場合は、
同じｐＨに調整するのに必要なＮａＯＨ量は３８ｇ−Ｎ
ａＯＨ／ｋｇ−ＣＯＤcrであった。これに対し、処理水
の循環を行わずにｐＨ調整した場合は、ＮａＯＨ必要量
は６２０ｇ−ＮａＯＨ／ｋｇ−ＣＯＤcrとなり、循環に
よりｐＨ調整に必要なアルカリ剤量を大幅に節減できる
ことが確認された。In Example 1, the amount of NaOH required for pH adjustment was 34 g-NaOH / kg-COD cr . On the other hand, when the treated water is circulated through the pipes 12 and 20 shown in FIG. 1 to the outflow water pipe (pipe 15) of the acid production tank,
The amount of NaOH required to adjust to the same pH is 38g-N
It was aOH / kg-COD cr . On the other hand, when the pH was adjusted without circulating the treated water, the required amount of NaOH was 620 g-NaOH / kg-COD cr , and it was confirmed that the amount of the alkaline agent required for pH adjustment could be significantly reduced by the circulation. It was
【００４４】[0044]
【発明の効果】以上詳述した通り、本発明の嫌気性処理
法によれば、焼酎廃液、ウイスキー蒸留廃液、ビール仕
込排水などの、窒素及びリンの栄養塩類を含む高濃度有
機性排水をＵＡＳＢ嫌気処理で効率的に処理して、有機
物と共に、窒素及びリンの同時除去を可能とすることが
でき、しかも、後段に凝集処理、硝化／脱窒などのプロ
セスを付加することが不要であるか又は付加しても小型
の装置で良く、処理効率及び処理コストが大幅に改善さ
れる。As described in detail above, according to the anaerobic treatment method of the present invention, highly concentrated organic wastewater containing nutrients of nitrogen and phosphorus such as shochu waste liquid, whiskey distillation waste liquid, beer charging wastewater, etc. can be treated with UASB. Is it possible to efficiently remove nitrogen and phosphorus together with organic substances by efficiently performing anaerobic treatment, and is it unnecessary to add processes such as coagulation treatment and nitrification / denitrification in the subsequent stage? Alternatively, even if added, a small device is sufficient, and the processing efficiency and the processing cost are significantly improved.
【００４５】さらに、グラニュール汚泥の浮上、流出を
防止して、ＵＡＳＢ反応槽の菌体保持量を著しく高く維
持することもできることから、高負荷処理による効率的
な処理が可能である。Furthermore, since it is possible to prevent the floating and outflow of the granulated sludge and maintain the cell retention amount in the UASB reaction tank to be remarkably high, it is possible to perform efficient treatment by high load treatment.
【図１】本発明の嫌気性処理法の一実施例方法を説明す
る系統図である。FIG. 1 is a system diagram illustrating a method of an embodiment of an anaerobic treatment method of the present invention.
１ 酸生成槽 ２ ＵＡＳＢ反応槽 1 acid production tank 2 UASB reaction tank
Claims (1)
生成槽で処理した後、ＵＡＳＢ型メタン生成槽で処理す
る方法において、 酸生成槽の流入水又は流出水にマグネシウム塩を添加す
ると共に、ＵＡＳＢ型メタン生成槽の流入水のｐＨを
５．８〜６．５に調整することを特徴とする嫌気性処理
法。1. A method of treating organic wastewater containing nitrogen and phosphorus in an acid generating tank and then treating it in a UASB type methane generating tank, wherein magnesium salt is added to inflow water or outflow water of the acid generating tank. , An anaerobic treatment method, characterized in that the pH of the inflow water of the UASB type methane production tank is adjusted to 5.8 to 6.5.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29129794A JP3358348B2 (en) | 1994-11-25 | 1994-11-25 | Anaerobic treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP29129794A JP3358348B2 (en) | 1994-11-25 | 1994-11-25 | Anaerobic treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH08141592A true JPH08141592A (en) | 1996-06-04 |
| JP3358348B2 JP3358348B2 (en) | 2002-12-16 |
Family
ID=17767070
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP29129794A Expired - Fee Related JP3358348B2 (en) | 1994-11-25 | 1994-11-25 | Anaerobic treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP3358348B2 (en) |
Cited By (11)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10118687A (en) * | 1996-10-22 | 1998-05-12 | Unitika Ltd | Treatment method of organic wastewater |
| JP2000167587A (en) * | 1998-12-02 | 2000-06-20 | Hitachi Plant Eng & Constr Co Ltd | Method and apparatus for anaerobic biological treatment of organic solid-containing waste water |
| JP2001038378A (en) * | 1999-07-29 | 2001-02-13 | Sumitomo Heavy Ind Ltd | Method and device for anaerobically treating organic waste water |
| JP2001252687A (en) * | 2000-03-10 | 2001-09-18 | Kurita Water Ind Ltd | Anaerobic treatment method for waste water from plant extraction |
| JP2003033781A (en) * | 2001-07-24 | 2003-02-04 | Sanki Eng Co Ltd | System for methane gas production |
| JP2005193189A (en) * | 2004-01-09 | 2005-07-21 | Kurita Water Ind Ltd | Anaerobic treatment method and anaerobic treatment apparatus |
| JP2006087986A (en) * | 2004-09-21 | 2006-04-06 | Kaneka Corp | Scale generation prevention method |
| JP2012076001A (en) * | 2010-09-30 | 2012-04-19 | Kuraray Co Ltd | Anaerobic wastewater treatment apparatus |
| JP2013208594A (en) * | 2012-03-30 | 2013-10-10 | Suntory Holdings Ltd | Method and apparatus for anaerobic wastewater treatment of organic wastewater |
| JP2018164890A (en) * | 2017-03-28 | 2018-10-25 | 住友重機械エンバイロメント株式会社 | Water treatment apparatus |
| CN110498578A (en) * | 2019-09-25 | 2019-11-26 | 厦门海洋职业技术学院 | A kind of recovery method of fats and oils processing high phosphorus Phosphorus From Wastewater |
-
1994
- 1994-11-25 JP JP29129794A patent/JP3358348B2/en not_active Expired - Fee Related
Cited By (13)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH10118687A (en) * | 1996-10-22 | 1998-05-12 | Unitika Ltd | Treatment method of organic wastewater |
| JP2000167587A (en) * | 1998-12-02 | 2000-06-20 | Hitachi Plant Eng & Constr Co Ltd | Method and apparatus for anaerobic biological treatment of organic solid-containing waste water |
| JP2001038378A (en) * | 1999-07-29 | 2001-02-13 | Sumitomo Heavy Ind Ltd | Method and device for anaerobically treating organic waste water |
| JP2001252687A (en) * | 2000-03-10 | 2001-09-18 | Kurita Water Ind Ltd | Anaerobic treatment method for waste water from plant extraction |
| JP2003033781A (en) * | 2001-07-24 | 2003-02-04 | Sanki Eng Co Ltd | System for methane gas production |
| JP4501432B2 (en) * | 2004-01-09 | 2010-07-14 | 栗田工業株式会社 | Anaerobic treatment method and apparatus |
| JP2005193189A (en) * | 2004-01-09 | 2005-07-21 | Kurita Water Ind Ltd | Anaerobic treatment method and anaerobic treatment apparatus |
| JP2006087986A (en) * | 2004-09-21 | 2006-04-06 | Kaneka Corp | Scale generation prevention method |
| JP4565945B2 (en) * | 2004-09-21 | 2010-10-20 | 株式会社カネカ | Scale generation prevention method |
| JP2012076001A (en) * | 2010-09-30 | 2012-04-19 | Kuraray Co Ltd | Anaerobic wastewater treatment apparatus |
| JP2013208594A (en) * | 2012-03-30 | 2013-10-10 | Suntory Holdings Ltd | Method and apparatus for anaerobic wastewater treatment of organic wastewater |
| JP2018164890A (en) * | 2017-03-28 | 2018-10-25 | 住友重機械エンバイロメント株式会社 | Water treatment apparatus |
| CN110498578A (en) * | 2019-09-25 | 2019-11-26 | 厦门海洋职业技术学院 | A kind of recovery method of fats and oils processing high phosphorus Phosphorus From Wastewater |
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|---|---|
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