JPH09248593A - Alkali consumption reducing method in uasb waste water treatment and device using same - Google Patents
Alkali consumption reducing method in uasb waste water treatment and device using sameInfo
- Publication number
- JPH09248593A JPH09248593A JP5743696A JP5743696A JPH09248593A JP H09248593 A JPH09248593 A JP H09248593A JP 5743696 A JP5743696 A JP 5743696A JP 5743696 A JP5743696 A JP 5743696A JP H09248593 A JPH09248593 A JP H09248593A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- uasb
- treated water
- water
- chamber
- 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
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- Y02W10/12—
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、ＵＡＳＢ (Upflow Ana
erobic Sludge Blanket)法を用いた有機性廃水処理にお
けるアルカリ消費量低減化方法およびこれに用いる装置
に関する。BACKGROUND OF THE INVENTION The present invention relates to UASB (Upflow Ana
The present invention relates to a method for reducing alkali consumption in an organic wastewater treatment using the erobic Sludge Blanket method and an apparatus used for the method.
【０００２】[0002]
【従来の技術および発明が解決しようとする課題】ＵＡ
ＳＢ法により有機性廃水を処理する場合、廃水中の有機
物は、働きの異なる３種類の嫌気性微生物によって最終
的にメタンガス、二酸化炭素および水になる。具体的に
は、まず、加水分解菌によって高分子有機物がアミノ
酸、糖、アルコールなどに分解され、次に、これら分解
物は酸生成菌によって酢酸などの低級脂肪酸、二酸化炭
素および水素などになる。そして、これら生成物は最終
的にメタン生成菌によってメタン、二酸化炭素および水
となる。PRIOR ART AND PROBLEMS TO BE SOLVED BY THE INVENTION UA
When treating the organic wastewater by the SB method, the organic matter in the wastewater finally becomes methane gas, carbon dioxide and water by the three kinds of anaerobic microorganisms having different functions. Specifically, first, a high molecular weight organic substance is decomposed into amino acids, sugars, alcohols and the like by hydrolyzing bacteria, and then these decomposed products are converted into lower fatty acids such as acetic acid, carbon dioxide and hydrogen by acid producing bacteria. Then, these products finally become methane, carbon dioxide, and water by the methanogen.
【０００３】上記廃水処理における酸生成過程におい
て、酢酸などの低級脂肪酸および水素の生成によって処
理水のｐＨが低下するので、その後段のメタン生成過程
を円滑に行うことができるように、処理水にアルカリ剤
を加えてｐＨを中性にする必要がある。During the acid generation process in the above wastewater treatment, the pH of the treated water is lowered by the production of lower fatty acids such as acetic acid and hydrogen, so that the treated water is treated so that the subsequent methane production process can be carried out smoothly. It is necessary to add an alkaline agent to make the pH neutral.
【０００４】この場合、アルカリ剤の添加は、ＵＡＳＢ
槽における処理の前段で行う必要があるが、有機性廃水
の性状によっては、処理水を中性化するのに多量のアル
カリ剤が必要となる。そのため、処理コストが非常に高
くなるという問題があった。本発明の目的は、上記の点
に鑑み、アルカリの消費量を低減し、処理コストを節減
することができるＵＡＳＢ廃水処理法を提供することに
ある。In this case, the addition of the alkaline agent is UASB
Although it needs to be performed before the treatment in the tank, a large amount of alkaline agent is required to neutralize the treated water depending on the properties of the organic wastewater. Therefore, there is a problem that the processing cost becomes very high. In view of the above points, an object of the present invention is to provide a UASB wastewater treatment method capable of reducing the consumption of alkali and reducing the treatment cost.
【０００５】また、本発明方法を実施するための装置と
して、図３に示す装置が考えられる。これは、原水が流
入する酸生成槽(31)、その後段のＵＡＳＢ槽(32)および
その後段の処理水槽(33)を具備したものであって、処理
水は、酸生成槽(31)から供給ポンプ(34)を介してＵＡＳ
Ｂ槽(32)へ送られる一方、ＵＡＳＢ槽(32)の後段の処理
水槽(33)から処理水の一部が循環ポンプ(35)を介して酸
生成槽(31)に還流されるものである。As an apparatus for carrying out the method of the present invention, the apparatus shown in FIG. 3 can be considered. This is equipped with an acid generation tank (31) into which raw water flows, a UASB tank (32) in the subsequent stage and a treated water tank (33) in the subsequent stage, and the treated water is supplied from the acid generation tank (31). UAS via supply pump (34)
While being sent to the B tank (32), a part of the treated water is returned from the treated water tank (33) after the UASB tank (32) to the acid generation tank (31) via the circulation pump (35). is there.
【０００６】しかしながら、上記処理装置の場合、処理
水槽(33)および循環ポンプ(35)が新たに必要となるた
め、建設費が高くつくと共に装置自体が大型化するとい
う問題があった。However, in the case of the above-mentioned treatment equipment, since the treatment water tank (33) and the circulation pump (35) are newly required, there is a problem that the construction cost becomes high and the equipment itself becomes large.
【０００７】本発明の今１つの目的は、このような点か
ら、建設費を節減できるＵＡＳＢ廃水処理装置を提供す
ることにある。[0007] Another object of the present invention is to provide a UASB wastewater treatment apparatus which can reduce the construction cost from the above point.
【０００８】[0008]
【課題を解決するための手段】本発明によるＵＡＳＢ廃
水処理法は、ＵＡＳＢ槽から出た処理水の一部をＵＡＳ
Ｂ槽の上流側へ戻して、該処理水を還流させることを特
徴とするものである。処理水の還流量は、廃水の性状に
より異なり、具体的には廃水の性状から求めたＵＡＳＢ
槽への廃水流入許容量に基づいて決定される。In the method for treating UASB wastewater according to the present invention, a part of the treated water discharged from the UASB tank is subjected to UAS.
It is characterized in that the treated water is returned to the upstream side of the tank B to be refluxed. The recirculation amount of treated water varies depending on the properties of wastewater, and specifically, the UASB obtained from the properties of wastewater.
It is determined based on the allowable amount of waste water flowing into the tank.
【０００９】本発明によるＵＡＳＢ廃水処理法における
アルカリ消費量低減化装置は、上記処理方法に直接使用
するものであって、原水の加水分解処理、酸生成を行う
調整槽(21)と、調整槽(21)の後段でメタン発酵を行うＵ
ＡＳＢ槽(2) とを備え、調整槽(21)は、仕切り壁(4) に
よって、原水が流入する原水供給室(21a) とＵＡＳＢ槽
(2) から処理水が流入する処理水室(21b) とに分けら
れ、仕切り壁(4) に処理水室(21b) の処理水の一部を原
水供給室(21a) へ還流させる通水孔(5) が形成され、処
理水室(21b) への処理水の流量が原水供給室(21a) への
原水の供給量より多くなるようになされていることを特
徴とするものである。The alkali consumption reducing apparatus in the UASB wastewater treatment method according to the present invention is used directly in the above treatment method, and comprises an adjusting tank (21) for hydrolyzing raw water and generating an acid, and an adjusting tank. (21) U which performs methane fermentation in the latter stage
The adjustment tank (21) is equipped with an ASB tank (2), and the partition wall (4) is used to feed the raw water into the raw water supply chamber (21a) and the UASB tank.
It is divided into a treated water chamber (21b) into which treated water flows from (2), and a part of the treated water in the treated water chamber (21b) is returned to the raw water supply chamber (21a) through the partition wall (4). The holes (5) are formed so that the flow rate of the treated water to the treated water chamber (21b) is larger than that of the raw water supplied to the raw water supply chamber (21a).
【００１０】[0010]
【発明の実施の形態】次に、本発明の実施形態について
説明する。図１に示すように、酸生成槽(1) において、
該槽に流入する有機性廃水中の高分子有機物を加水分解
菌によってアミノ酸、糖、アルコールなどに分解した
後、これら分解物から酸生成菌によって酢酸などの低級
脂肪酸、二酸化炭素および水素などを生成する。次に、
この廃水を給送ポンプ(3) でＵＡＳＢ槽(2) に送り、同
槽において酢酸などの低級脂肪酸、二酸化炭素および水
素などを最終的にメタン生成菌によってメタン化する。Next, an embodiment of the present invention will be described. As shown in Fig. 1, in the acid production tank (1),
After decomposing the high molecular weight organic matter in the organic wastewater flowing into the tank into amino acids, sugars, alcohols, etc. by hydrolyzing bacteria, lower fatty acids such as acetic acid, carbon dioxide and hydrogen are produced from these decomposed products by acid-producing bacteria. To do. next,
This wastewater is sent to a UASB tank (2) by a feed pump (3), and lower fatty acids such as acetic acid, carbon dioxide and hydrogen are finally methanated by methanogens.
【００１１】そして、ＵＡＳＢ槽(2) から出た処理水の
一部を循環ポンプで酸生成槽(1) に還流することによ
り、酸生成槽(1) のｐＨを上昇させ、これをＵＡＳＢ槽
(2) へ供給する。酸生成槽(1) への有機性廃水の供給量
をａ（ｍ3 ／日）とすると、処理水の還流量はａ〜３ａ
（ｍ3 ／日）とするのが一般的である。Then, a part of the treated water discharged from the UASB tank (2) is refluxed to the acid generation tank (1) by a circulation pump to increase the pH of the acid generation tank (1), and the pH of the UASB tank is increased.
Supply to (2). Assuming that the supply amount of the organic waste water to the acid generation tank (1) is a (m 3 / day), the reflux amount of the treated water is a to 3a.
(M 3 / day) is generally used.
【００１２】ＵＡＳＢ槽(2) の前段で酸生成槽(1) にア
ルカリ剤を加えて原水を中和する。上記処理水の還流に
よって処理水のｐＨがすでにある程度上昇されているた
め、アルカリ消費量は低減することとなる。具体的に
は、アルカリ剤として加えられた苛性ソーダの減少量は
廃水の性状によって異なるが、処理水の還流を行わない
場合に比べて３０〜５０％減少した事例がある。Before the UASB tank (2), an alkaline agent is added to the acid production tank (1) to neutralize the raw water. Since the pH of the treated water has already been raised to some extent by the reflux of the treated water, the amount of alkali consumed will be reduced. Specifically, the amount of caustic soda added as an alkaline agent varies depending on the properties of the wastewater, but there is a case where the amount of caustic soda is reduced by 30 to 50% compared to the case where the treated water is not refluxed.
【００１３】次に、上記方法を実施するためのアルカリ
消費量低減化装置について述べる。図２に示すように、
本装置は、原水の加水分解処理、酸生成を行う調整槽(2
1)と、調整槽(21)の後段でメタン発酵を行うＵＡＳＢ槽
(2) とを備えている。調整槽(21)は、垂直仕切り壁(4)
によって原水供給室(21a) と処理水室(21b) に分けられ
ている。原水供給室(21a) では、原水が流入して加水分
解処理および酸生成が行われ、処理水室(21b) には、Ｕ
ＡＳＢ槽(2) からオーバーフローした処理水が流入して
来る。Next, an alkali consumption reducing apparatus for carrying out the above method will be described. As shown in FIG.
This equipment is used in the adjustment tank (2
UASB tank for methane fermentation in 1) and after the adjusting tank (21)
(2) and are provided. The adjusting tank (21) has a vertical partition wall (4).
It is divided into a raw water supply room (21a) and a treated water room (21b). Raw water is introduced into the raw water supply chamber (21a) for hydrolysis treatment and acid generation, and U is supplied to the treated water chamber (21b).
Treated water that has overflowed from the ASB tank (2) flows in.
【００１４】仕切り壁(4) の底部には通水孔(5) が形成
されている。そして、処理水室(21b) への処理水流入量
(b) を原水供給室(21a) への原水供給量(a) より多く
し、処理水室(21b) の処理水の一部を通水孔(5) を経て
原水供給室(21a) へ常時還流させる。これによって、原
水が処理水室(21b) から未処理のまま系外へ流出するの
が防止される。A water passage hole (5) is formed at the bottom of the partition wall (4). And the amount of treated water flowing into the treated water chamber (21b)
(b) is made larger than the raw water supply amount (a) to the raw water supply chamber (21a), and part of the treated water in the treated water chamber (21b) is passed through the water passage hole (5) to the raw water supply chamber (21a). Always recirculate. This prevents raw water from flowing out of the system from the treated water chamber (21b) without being treated.
【００１５】ＵＡＳＢ槽(2) の前段で原水供給室(21a)
にアルカリ剤を加えて原水を中和する。ＵＡＳＢ槽(2)
では調整槽(21)から来る廃水がメタン発酵によって処理
される。Raw water supply chamber (21a) in front of UASB tank (2)
Add an alkaline agent to neutralize the raw water. UASB tank (2)
Now the wastewater coming from the tank (21) is treated by methane fermentation.
【００１６】ＵＡＳＢ槽(2) から処理水室(21b) へ流入
する処理水のうち、原水の供給量(a) と同量の処理水が
処理水室(21b) からオーバーフローし、系外へ流出す
る。Of the treated water flowing into the treated water chamber (21b) from the UASB tank (2), the same amount of treated water as the raw water supply amount (a) overflows from the treated water chamber (21b) and goes out of the system. leak.
【００１７】原水供給室(21a) への原水流入量(a) およ
び処理水室(21b) への処理水流入量(b) は、有機性廃水
の性状によって適宜変更する。The raw water inflow amount (a) into the raw water supply chamber (21a) and the treated water inflow amount (b) into the treated water chamber (21b) are appropriately changed depending on the properties of the organic wastewater.
【００１８】[0018]
【発明の効果】本発明方法はＵＡＳＢ槽から出た処理水
の一部をＵＡＳＢ槽の上流側へ戻して、該処理水を還流
させるものであり、この場合、ＵＡＳＢ槽から出る処理
水には、ＨＣＯ3 - イオンが多量に含まれているため、
この処理水をＵＡＳＢ槽の上流側における酸生成槽また
は調整槽に還流させることにより、下式の平衡が右に進
んでｐＨが上昇する。その結果、ＵＡＳＢ槽の前段で処
理水に加えられるアルカリの消費量を低減することがで
きる。According to the method of the present invention, a part of the treated water discharged from the UASB tank is returned to the upstream side of the UASB tank to recirculate the treated water. In this case, the treated water discharged from the UASB tank is , HCO 3 - because ions are contained in a large amount,
By refluxing this treated water to the acid production tank or the adjustment tank on the upstream side of the UASB tank, the equilibrium of the following formula advances to the right and the pH rises. As a result, it is possible to reduce the consumption of the alkali added to the treated water in the preceding stage of the UASB tank.
【００１９】[0019]
【化１】 また、本発明の装置は、原水の加水分解処理、酸生成を
行う調整槽と、調整槽の後段でメタン発酵を行うＵＡＳ
Ｂ槽とを備え、調整槽は、仕切り壁によって、原水が流
入する原水供給室とＵＡＳＢ槽から出た処理水が流入す
る処理水室に分けられ、処理水室への処理水の流入量が
原水供給室への原水の流入量より多くすることにより、
処理水室の処理水の一部が仕切り壁に形成された通水孔
を通って原水供給室へ流入するようにしたものであるか
ら、従来の処理水槽や循環ポンプを省略することが可能
となる。そのため、装置の建設費を抑えることができる
と共に装置の大型化の問題も解消される。Embedded image In addition, the apparatus of the present invention is a UAS that performs a methane fermentation in a regulating tank that performs hydrolysis treatment of raw water and acid generation, and a latter stage of the regulating tank.
The adjustment tank is divided into a raw water supply chamber into which raw water flows in and a treated water chamber into which treated water from the UASB tank flows, by a partition wall. By increasing the amount of raw water flowing into the raw water supply chamber,
Since a part of the treated water in the treated water chamber flows into the raw water supply chamber through the water holes formed in the partition wall, it is possible to omit the conventional treated water tank and circulation pump. Become. Therefore, the construction cost of the device can be suppressed, and the problem of increasing the size of the device can be solved.
【００２０】また、この装置を使用することによって、
ＵＡＳＢ槽の前流で原水に加えられるアルカリの消費量
を低減することができる。Further, by using this device,
It is possible to reduce the consumption of alkali added to the raw water in the upstream of the UASB tank.
【図１】本発明方法の一実施形態を示すフロースキーム
である。FIG. 1 is a flow scheme showing one embodiment of the method of the present invention.
【図２】本発明装置の一実施形態を示すフロースキーム
である。FIG. 2 is a flow scheme showing an embodiment of the device of the present invention.
【図３】従来の装置を示すフロースキームである。FIG. 3 is a flow scheme showing a conventional device.
(1) 酸生成槽 (2) ＵＡＳＢ槽 (3) 供給ポンプ (4) 仕切り壁 (5) 通水孔部 (21) 調整槽 (21a) 原水供給室 (21b) 処理水室 (1) Acid generation tank (2) UASB tank (3) Supply pump (4) Partition wall (5) Water passage hole (21) Adjustment tank (21a) Raw water supply room (21b) Treated water room
Claims (2)
ＳＢ槽の上流側へ戻して、該処理水を循環させることを
特徴とする、ＵＡＳＢ廃水処理法におけるアルカリ消費
量低減化方法。1. A part of the treated water discharged from the UASB tank is UA
A method for reducing alkali consumption in a UASB wastewater treatment method, characterized by returning the treated water to the upstream side of the SB tank and circulating the treated water.
槽(21)と、メタン発酵を行うＵＡＳＢ槽(2) とを備え、
調整槽(21)は、仕切り壁(4) によって、原水が流入する
原水供給室(21a) とＵＡＳＢ槽(2) から処理水が流入す
る処理水室(21b) とに分けられ、仕切り壁(4) に処理水
室(21b) の処理水の一部を原水供給室(21a) へ還流させ
る通水孔(5) が形成され、処理水室(21b) への処理水の
流量が原水供給室(21a) への原水の供給量より多くなる
ようになされていることを特徴とする、ＵＡＳＢ廃水処
理法におけるアルカリ消費量低減化装置。2. An adjustment tank (21) for hydrolysis treatment of raw water and acid production, and a UASB tank (2) for methane fermentation,
The regulating tank (21) is divided by the partition wall (4) into a raw water supply chamber (21a) into which raw water flows and a treated water chamber (21b) into which treated water flows from the UASB tank (2). A water passage hole (5) for returning part of the treated water in the treated water chamber (21b) to the raw water supply chamber (21a) is formed in 4), and the flow rate of treated water to the treated water chamber (21b) is A device for reducing alkali consumption in the UASB wastewater treatment method, which is characterized in that the amount of raw water supplied to the chamber (21a) is larger than that.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5743696A JPH09248593A (en) | 1996-03-14 | 1996-03-14 | Alkali consumption reducing method in uasb waste water treatment and device using same |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP5743696A JPH09248593A (en) | 1996-03-14 | 1996-03-14 | Alkali consumption reducing method in uasb waste water treatment and device using same |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09248593A true JPH09248593A (en) | 1997-09-22 |
Family
ID=13055612
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP5743696A Withdrawn JPH09248593A (en) | 1996-03-14 | 1996-03-14 | Alkali consumption reducing method in uasb waste water treatment and device using same |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09248593A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005125202A (en) * | 2003-10-22 | 2005-05-19 | Sumitomo Heavy Ind Ltd | Organic waste water treatment apparatus |
| JP2005262182A (en) * | 2004-03-22 | 2005-09-29 | Sumitomo Heavy Ind Ltd | Anaerobic treatment apparatus |
| WO2007078195A1 (en) * | 2006-01-05 | 2007-07-12 | Biothane Systems International B.V. | Process and reactor for anaerobic waste water purification |
| WO2007078194A1 (en) * | 2006-01-05 | 2007-07-12 | Biothane Systems International B.V. | Process and reactor for anaerobic waste water purification |
| KR101219494B1 (en) * | 2010-06-10 | 2013-01-11 | 한성국 | Pretreatment method of high concentrated ogranic sludges to applying for uasb |
| JP2013202601A (en) * | 2012-03-29 | 2013-10-07 | Osaka Gas Co Ltd | Method and device for treating organic waste water |
| JP2013208601A (en) * | 2012-03-30 | 2013-10-10 | Toshiba Corp | Water treatment system |
| JP2015120169A (en) * | 2015-03-30 | 2015-07-02 | 株式会社東芝 | Water treatment system |
-
1996
- 1996-03-14 JP JP5743696A patent/JPH09248593A/en not_active Withdrawn
Cited By (14)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005125202A (en) * | 2003-10-22 | 2005-05-19 | Sumitomo Heavy Ind Ltd | Organic waste water treatment apparatus |
| JP2005262182A (en) * | 2004-03-22 | 2005-09-29 | Sumitomo Heavy Ind Ltd | Anaerobic treatment apparatus |
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