JPH04326995A - Anaerobic water treatment apparatus - Google Patents
Anaerobic water treatment apparatusInfo
- Publication number
- JPH04326995A JPH04326995A JP3097146A JP9714691A JPH04326995A JP H04326995 A JPH04326995 A JP H04326995A JP 3097146 A JP3097146 A JP 3097146A JP 9714691 A JP9714691 A JP 9714691A JP H04326995 A JPH04326995 A JP H04326995A
- Authority
- JP
- Japan
- Prior art keywords
- reaction tank
- flocculant
- treated water
- tank
- 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.)
- Pending
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims abstract description 45
- 238000006243 chemical reaction Methods 0.000 claims abstract description 48
- 239000010802 sludge Substances 0.000 claims abstract description 31
- 239000002351 wastewater Substances 0.000 claims abstract description 15
- 230000003068 static effect Effects 0.000 claims abstract description 8
- 241001148471 unidentified anaerobic bacterium Species 0.000 claims abstract description 4
- 238000000034 method Methods 0.000 claims description 3
- 241000894006 Bacteria Species 0.000 abstract description 18
- VNWKTOKETHGBQD-UHFFFAOYSA-N methane Chemical compound C VNWKTOKETHGBQD-UHFFFAOYSA-N 0.000 abstract description 6
- 230000003179 granulation Effects 0.000 abstract description 5
- 238000005469 granulation Methods 0.000 abstract description 5
- 238000000855 fermentation Methods 0.000 abstract description 4
- 230000004151 fermentation Effects 0.000 abstract description 4
- 230000000630 rising effect Effects 0.000 abstract 2
- 230000003311 flocculating effect Effects 0.000 abstract 1
- 239000008187 granular material Substances 0.000 description 14
- 230000000717 retained effect Effects 0.000 description 5
- 238000002347 injection Methods 0.000 description 4
- 239000007924 injection Substances 0.000 description 4
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 3
- 230000000694 effects Effects 0.000 description 3
- 239000000203 mixture Substances 0.000 description 3
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 230000001580 bacterial effect Effects 0.000 description 2
- 239000000969 carrier Substances 0.000 description 2
- 239000000701 coagulant Substances 0.000 description 2
- 238000002474 experimental method Methods 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- 230000007774 longterm Effects 0.000 description 2
- 238000012545 processing Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 229920001661 Chitosan Polymers 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 241001148470 aerobic bacillus Species 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000008394 flocculating agent Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 239000000446 fuel Substances 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 229920001495 poly(sodium acrylate) polymer Polymers 0.000 description 1
- 238000012805 post-processing Methods 0.000 description 1
- 239000004576 sand Substances 0.000 description 1
- 238000004904 shortening Methods 0.000 description 1
- 239000000377 silicon dioxide Substances 0.000 description 1
- NNMHYFLPFNGQFZ-UHFFFAOYSA-M sodium polyacrylate Chemical compound [Na+].[O-]C(=O)C=C NNMHYFLPFNGQFZ-UHFFFAOYSA-M 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000009280 upflow anaerobic sludge blanket technology Methods 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Classifications
-
- Y02W10/12—
Abstract
Description
【０００１】［発明の目的］[Object of the invention]
【０００２】0002
【産業上の利用分野】本発明は、下水や産業廃水などの
有機性廃水を生物学的に処理する嫌気性水処理装置に関
するものである。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an anaerobic water treatment system for biologically treating organic wastewater such as sewage and industrial wastewater.
【０００３】0003
【従来の技術】嫌気性細菌であるメタン発酵細菌を用い
た嫌気性水処理方法は、好気性細菌を用いた活性汚泥法
などと比較して、余剰汚泥発生量が少ないこと、曝気の
ための動力が不要であること、メタンが発生するためエ
ネルギ回収が可能であること、などの利点がある。[Prior Art] Anaerobic water treatment methods using methane-fermenting bacteria, which are anaerobic bacteria, generate less surplus sludge than activated sludge methods using aerobic bacteria, and Advantages include that no power is required and that energy can be recovered since methane is generated.
【０００４】しかし、一方では、有機物の分解速度が遅
く、処理時間が長くかかるという欠点がある。このよう
な欠点を改善するために、メタン発酵細菌の高濃度化を
行い、処理時間の短縮を図った嫌気性水処理装置が提案
され、主に産業廃水などの高濃度廃水を対象として実用
化されつつある。However, on the other hand, it has the disadvantage that the decomposition rate of organic matter is slow and the processing time is long. In order to improve these shortcomings, an anaerobic water treatment device was proposed that increases the concentration of methane-fermenting bacteria and shortens the treatment time, and has been put into practical use mainly for high-concentration wastewater such as industrial wastewater. It is being done.
【０００５】これらの装置としては、担体の表面にメタ
ン発酵細菌を付着固定化した流動床形の水処理装置やメ
タン発酵細菌を自己造粒化した生物床形（ＵＡＳＢ形）
の水処理装置が知られている。These devices include a fluidized bed type water treatment device in which methane-fermenting bacteria are attached and immobilized on the surface of a carrier, and a biological bed type (UASB type) in which methane-fermenting bacteria are self-granulated.
water treatment equipment is known.
【０００６】流動床形の水処理装置は １００〜 ５０
０μｍ程度の担体を反応槽に充填し、廃水および処理水
循環液の上向流速によって担体流動層を形成させる装置
である。
担体の表面にはメタン発酵細菌が付着しており、廃水は
ここを流動する間に浄化される。用いられる担体はケイ
砂、セラミックス、活性炭などである。これらの粒子は
小さいので非常に大きな比表面積が得られ、このため高
濃度のメタン発酵細菌を反応槽内に保持し、効率のよい
処理を行うことができる。[0006] Fluidized bed type water treatment equipment has a rating of 100 to 50
This is an apparatus in which a reaction tank is filled with carriers having a diameter of approximately 0 μm, and a carrier fluidized bed is formed by the upward flow rate of waste water and treated water circulating fluid. Methane-fermenting bacteria are attached to the surface of the carrier, and the wastewater is purified while flowing through it. The carriers used are silica sand, ceramics, activated carbon, etc. Since these particles are small, a very large specific surface area can be obtained, and therefore, a high concentration of methane-fermenting bacteria can be retained in the reaction tank and efficient treatment can be performed.
【０００７】生物床形の水処理装置は、種汚泥（消化汚
泥）を反応槽に投入して、これを自己造粒化させたメタ
ン発酵細菌によって廃水の浄化を行う装置である。造粒
化は、廃水の上向流の流動や、発生する発酵ガス（主成
分はメタンおよび炭酸ガス）の上昇に伴う旋回運動によ
って徐々に起るものと考えられている。この造粒物は菌
体の塊と言ってよく、このため高濃度のメタン発酵細菌
が反応槽内に保持され、効率のよい処理を行うことがで
きる。A biological bed type water treatment device is a device in which seed sludge (digested sludge) is charged into a reaction tank, and wastewater is purified using methane-fermenting bacteria that self-granulate the seed sludge. It is believed that granulation occurs gradually due to the upward flow of wastewater and the swirling movement accompanying the rise of the generated fermentation gas (mainly methane and carbon dioxide gas). This granulated material can be said to be a mass of bacterial cells, and therefore, a high concentration of methane-fermenting bacteria is retained in the reaction tank, allowing efficient processing.
【０００８】[0008]
【発明が解決しようとする課題】上述したように流動床
形の水処理装置および生物床形の水処理装置は何れも高
濃度のメタン発酵細菌を保持でき、効率的な処理を行う
ことができるが、流動床形の水処理装置においては、そ
の反応槽立上げ時にメタン発酵細菌は担体にほとんど付
着していないので低い負荷で運転をせざるを得ず、メタ
ン発酵細菌が増殖して十分な量が担体に付着するまでに
６〜１２ヶ月の長期間を要し、この長期間設計負荷より
相当低い負荷での運転しかできないという欠点がある。[Problems to be Solved by the Invention] As mentioned above, both the fluidized bed type water treatment equipment and the biological bed type water treatment equipment can retain a high concentration of methane-fermenting bacteria and can perform efficient treatment. However, in fluidized bed water treatment equipment, when the reaction tank is started up, methane-fermenting bacteria are hardly attached to the carrier, so it has to be operated at a low load, and the methane-fermenting bacteria multiply and become insufficient. The disadvantage is that it takes a long period of 6 to 12 months for the amount to adhere to the carrier, and that it can only be operated at a load considerably lower than the long-term design load.
【０００９】また生物床形反応装置においても、造粒化
のメカニズムが未だ完全に解明されておらず、廃水の性
状によっては造粒化が困難な場合があり、さらに、造粒
化されるまで６〜１２ヶ月という長期間を要し、このた
め、流動床形水処理装置の場合と同様に、長期間設計負
荷より相当低い負荷でしか運転できないという欠点があ
る。[0009] Also, in biological bed reactors, the mechanism of granulation has not yet been completely elucidated, and depending on the properties of the wastewater, granulation may be difficult; It takes a long period of time, from 6 to 12 months, and therefore, as with fluidized bed water treatment plants, it has the disadvantage that it can only be operated at a load considerably lower than the long-term design load.
【００１０】本発明は上記の問題を考慮してなされたも
ので、メタン発酵細菌の造粒物を短時間に確実に形成さ
せ、設計負荷より低い負荷で運転される反応槽立上げ期
間を短縮できる合理的な嫌気性水処理装置を提供するこ
とを目的としている。［発明の構成］[0010] The present invention was made in consideration of the above-mentioned problems, and is capable of reliably forming granules of methane-fermenting bacteria in a short period of time, thereby shortening the start-up period of a reaction tank operated at a load lower than the design load. The purpose is to provide a rational anaerobic water treatment device that can [Structure of the invention]
【００１１】[0011]
【課題を解決するための手段及び作用】上記の目的を達
成するために、本発明は嫌気性細菌を内部に保持し、導
入された廃水を浄化する反応槽と、この反応槽を溢流し
た処理水を一旦貯留すると共に貯留された処理水の一部
を反応槽下部へ循環させる循環管路に接続されている処
理水槽と、上記循環管路内に凝集剤を添加する凝集剤添
加装置と、上記循環管路の凝集剤添加部の後段に設置さ
れたスタティックミキサを備えた水処理装置として構成
され、反応槽立上げの際に種汚泥（消化汚泥）を処理水
槽に所定量投入して循環ポンプによって反応槽下部へ循
環させ、また反応槽上部から溢流した汚泥を処理水槽へ
戻して種汚泥を反応槽と処理水槽の間で循環させると共
に循環ポンプの吐出側付近の配管内に凝集射を所定量添
加し、スタティックミキサで急速攪拌して汚泥と凝集剤
を均一に混合して反応槽下部へ流入させ、反応槽内で上
向流でゆっくり流動させ、種汚泥を徐々にフロック化し
て造粒し、このとき造粒物は沈降速度が大きいので反応
槽内の上向流に打ち勝って反応槽内に保持され、これに
よって高濃度のメタン発酵細菌を保持できるようにして
いる。[Means and effects for solving the problems] In order to achieve the above object, the present invention provides a reaction tank that retains anaerobic bacteria inside and purifies introduced wastewater, and a reaction tank that overflows this reaction tank. A treated water tank connected to a circulation pipe that temporarily stores the treated water and circulates a part of the stored treated water to the lower part of the reaction tank, and a flocculant addition device that adds a flocculant into the circulation pipe. , is configured as a water treatment device equipped with a static mixer installed after the flocculant addition section in the circulation pipe, and when starting up the reaction tank, a predetermined amount of seed sludge (digested sludge) is put into the treatment water tank. The sludge is circulated to the lower part of the reaction tank by the circulation pump, and the sludge that overflows from the upper part of the reaction tank is returned to the treatment tank, and the seed sludge is circulated between the reaction tank and the treatment tank, and it aggregates in the piping near the discharge side of the circulation pump. A predetermined amount of sludge is added and stirred rapidly using a static mixer to uniformly mix the sludge and flocculant, which then flows into the bottom of the reaction tank.Then, the seed sludge is gradually made into flocs by slowly flowing upward in the reaction tank. At this time, the granulated material has a high sedimentation rate, so it overcomes the upward flow in the reaction tank and is retained in the reaction tank, thereby making it possible to retain a high concentration of methane-fermenting bacteria.
【００１２】0012
【実施例】本発明の一実施例を図１に示す。図１におい
て、廃水は原水ポンプ１により原水導入管２を介して反
応槽３の下部から流入される。反応槽３の内部にはメタ
ン発酵細菌の造粒物が保持されており、流入した廃水が
上向流で流れる間にメタン発酵細菌の作用で浄化される
。浄化された廃水（処理水）は反応槽３の上部から溢流
し、溢流管路４を介して処理水槽５に流入し、さらに処
理水槽５を溢流した処理水は処理水管路１３を介して抜
き出され、河川などへ放流され、あるいは後処理装置へ
送られる。[Embodiment] An embodiment of the present invention is shown in FIG. In FIG. 1, wastewater is introduced from the lower part of a reaction tank 3 via a raw water introduction pipe 2 by a raw water pump 1. Granules of methane-fermenting bacteria are held inside the reaction tank 3, and the inflowing wastewater is purified by the action of the methane-fermenting bacteria while flowing upward. The purified wastewater (treated water) overflows from the upper part of the reaction tank 3 and flows into the treated water tank 5 via the overflow pipe 4, and the treated water that overflows the treated water tank 5 flows through the treated water pipe 13. The waste is extracted and discharged into rivers, etc., or sent to post-processing equipment.
【００１３】また処理水槽５内に貯留された処理水の一
部は循環ポンプ６により循環管路７を介して反応槽３へ
循環され、発生した発酵ガスは反応槽３の上部に設けら
れた発酵ガス管路８を介して取り出され、ガスホルダ９
に一度貯留された後、ガスボイラ（図示せず）などの燃
料として有効利用される。A part of the treated water stored in the treated water tank 5 is circulated to the reaction tank 3 via the circulation pipe 7 by a circulation pump 6, and the generated fermentation gas is supplied to the reaction tank 3. The fermentation gas is taken out via the pipe line 8 and placed in the gas holder 9.
Once stored, it is effectively used as fuel for gas boilers (not shown).
【００１４】また、反応槽立上げ時に、処理水槽５に投
入された種汚泥を循環ポンプ６で反応槽３に循環させる
循環管路７内に凝集剤を注入するための凝集剤注入ポン
プ１０および凝集剤タンク１１が設置され、さらに循環
管路７には循環している種汚泥と注入した凝集剤を均一
に混合するためのスタティックミキサ１２が設置されて
いる。[0014] Furthermore, at the time of starting up the reaction tank, a flocculant injection pump 10 and A flocculant tank 11 is installed, and a static mixer 12 is also installed in the circulation pipe 7 to uniformly mix the circulating seed sludge and the injected flocculant.
【００１５】処理水槽５に投入された種汚泥は循環管路
７内に注入された凝集剤とスタティックミキサ１２によ
って混合され、マイクロフロックを形成し、このマイク
ロフロックは反応槽３内をゆるやかに上向流で流動しな
がら凝集してフロックを形成し、さらにこのフロックが
相互に結合し、ミクロ的な流動の乱れによって旋回しな
がら造粒物を形成する。The seed sludge put into the treated water tank 5 is mixed with the flocculant injected into the circulation pipe 7 by the static mixer 12 to form micro flocs, and these micro flocs are slowly raised inside the reaction tank 3. While flowing in a countercurrent, they aggregate to form flocs, and these flocs are further bonded to each other and swirled due to microscopic turbulence in the flow to form granules.
【００１６】沈降速度が、反応槽３内の上向流速以上の
造粒物はリアクタ３内に留まり保持されるが、造粒物ま
で進行が進まなかったフロックや造粒物でも反応槽３内
の上向流速以下の沈降速度のものは反応槽３の上部から
溢流し、溢流管路４を介して処理水槽５に戻る。Granules whose sedimentation speed is higher than the upward flow velocity in the reaction tank 3 remain in the reactor 3 and are retained, but even flocs and granules that have not progressed to the granules still remain in the reaction tank 3. Water with a settling velocity lower than the upward flow velocity overflows from the upper part of the reaction tank 3 and returns to the treated water tank 5 via the overflow pipe 4.
【００１７】次に再び循環ポンプ６によって反応槽３に
循環されるが、この際にも注入されている凝集剤とスタ
ティックミキサ１２によって混合され、反応槽３へ循環
される。このような循環を繰返すことによって、反応槽
３内で種汚泥の造粒化が徐々に進行し、投入された種汚
泥全てが造粒物として反応槽３内に保持されるようにな
る。この時には反応槽３の上部には上澄域が生成し、上
澄液だけが循環するようになる。この後廃水を原水ポン
プ１によって反応槽３に流入させるのを開始し、廃水の
浄化を行う。Next, it is circulated to the reaction tank 3 again by the circulation pump 6, but at this time as well, it is mixed with the flocculant that has been injected by the static mixer 12, and the mixture is circulated to the reaction tank 3. By repeating such circulation, granulation of the seed sludge gradually progresses in the reaction tank 3, and all of the seed sludge introduced is retained in the reaction tank 3 as granules. At this time, a supernatant region is generated in the upper part of the reaction tank 3, and only the supernatant liquid is circulated. After that, the raw water pump 1 starts flowing the wastewater into the reaction tank 3, and the wastewater is purified.
【００１８】ここで処理水槽５に投入される種汚泥量は
、反応槽３内を上向流で流動する汚泥の濃度が １，０
００〜 ８，０００ｍｇＶＳＳ／リットルになるように
調整することが望ましい。この汚泥濃度が小さすぎたり
、また大きすぎたりすると反応槽３内での凝集反応がう
まく進行せず、造粒化しにくくなる。また種汚泥として
は下水処理場や廃水処理施設の消化汚泥が望ましい。Here, the amount of seed sludge introduced into the treated water tank 5 is such that the concentration of the sludge flowing upward in the reaction tank 3 is 1.0.
It is desirable to adjust it to 00 to 8,000 mgVSS/liter. If this sludge concentration is too small or too large, the flocculation reaction within the reaction tank 3 will not proceed well, making it difficult to granulate the sludge. Digested sludge from sewage treatment plants and wastewater treatment facilities is also desirable as the seed sludge.
【００１９】用いる凝集剤としてはメタン発酵細菌の活
性に悪影響を及ぼさないことが重要であり、例えばポリ
アクリル酸ナトリウム、キトサン系凝集剤、ＰＡＣなど
が望ましい。用いる種汚泥の性状によって最適な凝集剤
の種類および注入量が異なるので予備実験によって適当
なものを選定することが望ましい。大略の凝集剤注入量
は固形物重量当り ０．１〜８％である。It is important that the flocculant used does not adversely affect the activity of the methane-fermenting bacteria; for example, sodium polyacrylate, chitosan-based flocculants, PAC, etc. are preferable. Since the optimal type and injection amount of flocculant vary depending on the properties of the seed sludge used, it is desirable to select an appropriate flocculant through preliminary experiments. The approximate amount of flocculant injected is 0.1 to 8% based on the weight of solids.
【００２０】さらに反応槽３内の上向流速も造粒物の形
成には重要な因子であるが、反応槽の形状や用いる種汚
泥、凝集剤によって最適な値が異なるため、予備実験に
よって決める必要がある。大略の上向流速は ０．１〜
１０ｍ／Ｈである。また、造粒物の形成時間は凝集剤の
種類と注入量、種汚泥投入量などの条件によって異なる
が大略数時間から数日の短期間となる。Furthermore, the upward flow velocity in the reaction tank 3 is also an important factor for the formation of granules, but the optimum value varies depending on the shape of the reaction tank, the seed sludge used, and the flocculant, so it is determined by preliminary experiments. There is a need. The approximate upward flow velocity is 0.1~
It is 10m/H. Further, the time for forming granules varies depending on conditions such as the type of flocculant, the amount of injection, and the amount of seed sludge input, but it is generally a short period of several hours to several days.
【００２１】[0021]
【発明の効果】以上説明したように本発明によれば、メ
タン発酵細菌の造粒物を短期間で確実に形成させること
ができるので、高濃度の菌体を反応槽立上げ時に保持す
ることができ、従って設計負荷での運転ができるように
なるまでの反応槽立上げ期間を大幅に短縮することが可
能となる。[Effects of the Invention] As explained above, according to the present invention, granules of methane-fermenting bacteria can be reliably formed in a short period of time, so that a high concentration of bacterial cells can be maintained at the time of starting up the reaction tank. Therefore, it is possible to significantly shorten the reaction tank start-up period until it can be operated at the design load.
【図１】本発明による嫌気性水処理装置の一実施例を示
す構成図。FIG. 1 is a configuration diagram showing an embodiment of an anaerobic water treatment apparatus according to the present invention.
１…原水ポンプ、３…反応槽、５…処理水槽、６…循環
ポンプ、１０…凝集剤注入ポンプ、１１…凝集剤タンク
、１２…スタティックミキサ。DESCRIPTION OF SYMBOLS 1... Raw water pump, 3... Reaction tank, 5... Treated water tank, 6... Circulation pump, 10... Coagulant injection pump, 11... Coagulant tank, 12... Static mixer.
Claims (1)
た廃水を生化学的に処理する反応槽と、反応槽から溢流
した処理水を一時的に貯留すると共に、貯留された処理
水の一部を反応槽の下部へ循還させる処理水槽と、処理
水槽から反応槽への循環管路内に、装置の立上げ時に処
理水槽に投入された種汚泥を凝集させる凝集剤を添加す
る凝集剤添加装置と、循環管路の凝集剤添加部の後段に
設置され、種汚泥と凝集剤とを混合させるスタティック
ミキサを備えたことを特徴とする嫌気性水処理装置。Claim 1: A reaction tank that retains anaerobic bacteria inside and biochemically processes introduced wastewater, and temporarily stores treated water that overflows from the reaction tank, as well as the stored treated water. A flocculant that flocculates the seed sludge that is put into the treated water tank when the equipment is started up is added to the treated water tank that circulates a portion of the sludge to the lower part of the reaction tank, and in the circulation pipe from the treated water tank to the reaction tank. An anaerobic water treatment device comprising: a flocculant addition device; and a static mixer installed after the flocculant addition section in a circulation pipe to mix seed sludge and flocculant.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3097146A JPH04326995A (en) | 1991-04-26 | 1991-04-26 | Anaerobic water treatment apparatus |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3097146A JPH04326995A (en) | 1991-04-26 | 1991-04-26 | Anaerobic water treatment apparatus |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04326995A true JPH04326995A (en) | 1992-11-16 |
Family
ID=14184436
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3097146A Pending JPH04326995A (en) | 1991-04-26 | 1991-04-26 | Anaerobic water treatment apparatus |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04326995A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008086862A (en) * | 2006-09-29 | 2008-04-17 | Nippon Paper Industries Co Ltd | Anaerobic treatment method and arrangement |
| JP2008279383A (en) * | 2007-05-11 | 2008-11-20 | Kurita Water Ind Ltd | Method and apparatus for anaerobic treatment |
| JP2011115689A (en) * | 2009-12-01 | 2011-06-16 | Ishigaki Co Ltd | Nitrogen removal apparatus and method |
| JP2014100679A (en) * | 2012-11-21 | 2014-06-05 | Kuraray Co Ltd | Anaerobic wastewater treatment method using carrier |
| JP2014133210A (en) * | 2013-01-10 | 2014-07-24 | Swing Corp | Anaerobic treatment method and anaerobic treatment apparatus of organic effluent |
| JP2016185523A (en) * | 2015-03-27 | 2016-10-27 | 住友重機械エンバイロメント株式会社 | Anaerobic treatment device |
| CN113788541A (en) * | 2021-09-30 | 2021-12-14 | 同济大学 | Method for promoting rapid granulation of anaerobic ammonium oxidation bacteria by using coagulant |
-
1991
- 1991-04-26 JP JP3097146A patent/JPH04326995A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2008086862A (en) * | 2006-09-29 | 2008-04-17 | Nippon Paper Industries Co Ltd | Anaerobic treatment method and arrangement |
| JP2008279383A (en) * | 2007-05-11 | 2008-11-20 | Kurita Water Ind Ltd | Method and apparatus for anaerobic treatment |
| JP2011115689A (en) * | 2009-12-01 | 2011-06-16 | Ishigaki Co Ltd | Nitrogen removal apparatus and method |
| JP2014100679A (en) * | 2012-11-21 | 2014-06-05 | Kuraray Co Ltd | Anaerobic wastewater treatment method using carrier |
| JP2014133210A (en) * | 2013-01-10 | 2014-07-24 | Swing Corp | Anaerobic treatment method and anaerobic treatment apparatus of organic effluent |
| JP2016185523A (en) * | 2015-03-27 | 2016-10-27 | 住友重機械エンバイロメント株式会社 | Anaerobic treatment device |
| CN113788541A (en) * | 2021-09-30 | 2021-12-14 | 同济大学 | Method for promoting rapid granulation of anaerobic ammonium oxidation bacteria by using coagulant |
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