JPS6279896A - Sewage treatment device - Google Patents
Sewage treatment deviceInfo
- Publication number
- JPS6279896A JPS6279896A JP60219054A JP21905485A JPS6279896A JP S6279896 A JPS6279896 A JP S6279896A JP 60219054 A JP60219054 A JP 60219054A JP 21905485 A JP21905485 A JP 21905485A JP S6279896 A JPS6279896 A JP S6279896A
- Authority
- JP
- Japan
- Prior art keywords
- carrier particles
- particles
- fluidized bed
- living
- reaction vessel
- 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
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
- Biological Treatment Of Waste Water (AREA)
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野ン
この発明は砂、ゼオライトなどを生物担体粒子とし、こ
′ｎ乞槽内で上向流する有機性汚水により流動状態に保
ち、この有機性汚水火好気式又は嫌気式に生物化学的に
処理する汚水処理装置に関する。Detailed Description of the Invention (Industrial Field of Application) This invention uses sand, zeolite, etc. as biological carrier particles, which are kept in a fluid state by organic sewage flowing upward in a tank. This invention relates to a sewage treatment device that biochemically treats sewage using an aerobic or anaerobic method.
、従来の技術）
この様な汚水処理装置は従来から公知であって、高負荷
で運転χ行５と比較的に早期に、又、長期間運転火打っ
ていると次第に、担体粒子の表面に過剰の生物膜が付着
し、生物担体粒子の見掛は比重が軽（なる。, Prior Art) Such sewage treatment equipment has been known for a long time, and it is known that when it is operated under high load, it is relatively early on, and when it is operated for a long time, it gradually forms on the surface of the carrier particles. Excess biofilm adheres, and the biocarrier particles appear to have a light specific gravity.
このため汚水の上向流の通水線速度ンそｎまで通りの一
定で通水すると生物膜が過剰に付着した生物担体粒子は
処理水に混って系外に流出し、処理水の水質χ悪化する
と共に槽内の粒子量は減少するので補充する必要がある
。そこで通水線速度χ遅（すると見掛は比重の軽い生物
膜が過剰に付着した生物担体粒子は流動床の上層に、見
掛比重の重い生物担体粒子は流動床の下層に集まり、下
層の流動が不充分になる。Therefore, if wastewater is passed at a constant linear velocity in the upward direction, the biological carrier particles with excessive biofilm attached will mix with the treated water and flow out of the system, resulting in the quality of the treated water. As χ deteriorates, the amount of particles in the tank decreases, so it is necessary to replenish it. Therefore, the linear water flow rate χ is slow (as a result, biological carrier particles with an excessively attached biofilm with an apparent light specific gravity gather in the upper layer of the fluidized bed, and biological carrier particles with a heavy apparent specific gravity gather in the lower layer of the fluidized bed. Flow becomes insufficient.
（発明が解決しようとする問題点）
このため生物膜が厚くなった生物担体粒子ン機械攪拌、
ポンプ攪拌で攪拌し、厚（付着しπ生物膜の膜厚欠調整
することが行わｎているが、この方法では剥離が強過ぎ
、担体粒子そのものまでも微細化してしまい、所定の膜
厚に調整することが容易でない。(Problem to be solved by the invention) For this reason, mechanical agitation of biological carrier particles with thickened biofilms,
The thickness of the biofilm is adjusted by stirring with a pump, but this method causes too much peeling and the carrier particles themselves become finer, making it impossible to reach the desired film thickness. Not easy to adjust.
（問題点ケ解決する＝めの手段）
そこで本発明は汚水処理装置として、生物担体粒子ケ内
蔵し、汚水欠生物化学的に処理する流動床式反応槽と、
該反応槽の流動床界面付近に開口した生物担体粒子の抜
出手段と、該抜出手段から出る生物担体粒子Ｘ受入′れ
る下部が逆円錐形の液体サイクロンと、該液体サイクロ
ンから担体粒子ゲ前記流動床式反応槽に返送する返送手
段とを有することン特徴とする。(Means for solving the problem) Therefore, the present invention provides a fluidized bed reaction tank as a sewage treatment device that incorporates biological carrier particles and performs biochemical treatment of sewage.
A biological carrier particle extracting means opened near the fluidized bed interface of the reaction tank; a hydrocyclone having an inverted conical lower part for receiving biological carrier particles X coming out from the extracting means; It is characterized in that it has a return means for returning to the fluidized bed type reaction tank.
（作 用）
反応槽内で生物膜が厚（付着しπ生物担体粒子は流動床
の上部に到達し、抜出手段で逐次液体サイクロンに抜出
さｎ、液体サイクロンで攪拌さｎて膜厚ン薄（調整さｎ
、調整さｒした生物担体粒子は返送手段により反応槽内
に返送される。(Function) When the biofilm thickens (attaches) in the reaction tank, the biocarrier particles reach the top of the fluidized bed and are sequentially extracted into the liquid cyclone by the extraction means, and then stirred by the liquid cyclone to increase the film thickness. thin (adjusted n
The adjusted biological carrier particles are returned to the reaction tank by a return means.
（実施例）
図示の実施例において、／は嫌気式処理用の反応槽、Ｊ
は槽内で生物担体粒子により４３成さｎ ｙ、＝流動床
、３は抜出手段、グは下部が逆円錐形の液体サイクロン
、５は返送手段〉示す。(Example) In the illustrated example, / is a reaction tank for anaerobic treatment, J
is a fluidized bed formed by biological carrier particles in a tank, 3 is an extraction means, g is a hydrocyclone with an inverted conical lower part, and 5 is a return means.
汚水は槽内で生物担体粒子に流動床欠杓成させる１こめ
供給管６で槽内底部に供給さｎ、生物担体粒子ケ流動化
しながら流動床中ン上向流する際に粒子表面の生物によ
って生物化学的に処理さｎ１処理水となって槽頂部の排
水管りに排水される。The sewage is fed to the bottom of the tank through a supply pipe 6 to form a fluidized bed on the biological carrier particles in the tank, and the biological carrier particles are fluidized and flow upward into the fluidized bed. The water is biochemically treated as n1 treated water and drained into the drain pipe at the top of the tank.
抜出手段３は上端が流動床コの界面２′付近のレベルで
槽壁に接続した傾斜管で、途中に開閉弁Ｖ１ヶ有し、下
端は液体サイクロンダに開口している。The extraction means 3 is an inclined pipe whose upper end is connected to the tank wall at a level near the interface 2' of the fluidized bed, and has an on-off valve V1 in the middle, and whose lower end opens into the hydrocyclonder.
液体サイクロンダは下部が逆円錐形の容器の下端部内に
ポンプＰで液体ケ接線方向に注入し、内部に生じ・ｂ液
の旋回流で生物担体粒子Ｘ受入する。この実施例ではポ
ンプが注入する液はサイクロン内から取水し、循環する
様になっている。The hydrocyclonder uses a pump P to inject liquid tangentially into the lower end of a container whose lower part has an inverted conical shape, and receives biological carrier particles X in the swirling flow of liquid b generated inside. In this embodiment, the liquid injected by the pump is taken from within the cyclone and circulated.
そして、液体サイクロンダの容器上部には開閉弁Ｖ２乞
有する水抜管ｇが接続し、器内の液を凝集槽デに排水で
きる様にしである。又、サイクロンの下端出口は開閉弁
Ｖｓ Ｙ介して圧力水が注入さｎろ移送槽１０Ｋ通じ、
返送手段！としての管は途中に開閉弁Ｖ４欠有し、上記
移送槽１０の下端出口と反応槽／の底部ン接続する。A drain pipe g having an on-off valve V2 is connected to the upper part of the container of the hydrocyclonder, so that the liquid inside the container can be drained to the coagulation tank. In addition, pressure water is injected into the lower end outlet of the cyclone through the on-off valve VsY, which is connected to the filtration transfer tank 10K.
Return method! The pipe has an on-off valve V4 in the middle and connects the lower end outlet of the transfer tank 10 to the bottom of the reaction tank.
移送槽ｉｏの上部には弁Ｖ５ン有する圧力水供給手段／
３が接続しである。At the top of the transfer tank io there is a pressure water supply means having a valve V5.
3 is connected.
運転火打うには弁Ｖ＋ Ｙ開、他の弁乞閉にして反応槽
内の液とともに生物膜が厚（付着した生物担体粒子ケ液
体すイクロン亭に抜出手段３で入れる。To start operation, open the valves V+Y and close the other valves, and the biofilm with the liquid in the reaction tank (attached biological carrier particles) is put into the liquid suction tube by the extraction means 3.
サイクロン内にはｙ所定量の生物担体粒子が溜ったら弁
Ｖ＋ Ｙ閉じ、ポンプＰＹ運転して前述の様に液体の旋
回流で粒子火攪拌し、付着する生物膜の膜厚ン薄（調整
する。When a predetermined amount of biocarrier particles have accumulated in the cyclone, valve V+Y is closed, pump PY is operated, and the particles are stirred by the swirling flow of the liquid as described above, and the thickness of the attached biofilm is adjusted. .
その所要時間は生物膜の膜厚にもよるが７〜／一時間程
度である。尚、容器下部の逆円錐形の頂角は担体粒子の
安息角より小さいｒｏ０以下が好ましく、又、ポンプＰ
が循環させろ水量は容器内で担体粒子が旋回状態で充分
に流動し、且つ容器内上部に担体の流動界面が形成さ几
る範囲がよい。The required time is about 7 to 1 hour, depending on the thickness of the biofilm. The apex angle of the inverted cone at the bottom of the container is preferably ro0 or less, which is smaller than the angle of repose of the carrier particles, and the pump P
The amount of water to be circulated is preferably within a range that allows the carrier particles to flow sufficiently in a swirling state within the container and to form a fluid interface of the carrier at the upper portion of the container.
液体サイクロンでの剥離が終ったらポンプ欠停め、サイ
クロン内の液、剥離した生物膜、担体粒子の丁べて欠返
送手段５で反応槽の底部に返送してもよいが、この実施
例では弁Ｖ２に開にしてサイクロン内の大部分の液と剥
離した生物膜を水抜管ざで凝集槽りに入１″Ｌ、こ〜で
高分子凝集剤などン薬注して生物膜に凝集したのち沈澱
槽／ｌに導いて沈澱させ、生物膜は汚泥として抜出し、
液は放流する。After the separation in the liquid cyclone is completed, the pump may be stopped, and the liquid in the cyclone, the separated biological film, and the carrier particles may be returned to the bottom of the reaction tank by the return means 5, but in this embodiment, the valve Open the cyclone to V2, put most of the liquid in the cyclone and the detached biofilm into a flocculation tank with a drainage pipe of 1"L, and pour a polymer flocculant into the tank to coagulate it into a biofilm. The biofilm is extracted as sludge, and the biofilm is extracted as sludge.
Discharge the liquid.
サイクロン内に残つに生物担体粒子は弁Ｖ３欠開いて移
送槽１０に流下させ、次いで弁Ｖｓｋ閉、弁ｖ４、Ｖｓ
Ｙ開にし、圧力水χ圧力水供給手段／３から柳７０内に
注入し、この圧力水で生物担体粒子大返送手段Ｓ火通じ
反応槽の底物内に返送する。The biological carrier particles remaining in the cyclone are caused to flow down into the transfer tank 10 by opening the valve V3, then closing the valve Vsk, and closing the valves V4 and Vs.
Y is opened, pressure water χ is injected into the willow 70 from the pressure water supply means /3, and the pressure water is returned to the bottom of the reaction tank through the large biological carrier particle return means S.
圧力水には排水管７から出ろ処理水や、供給管６で反応
槽に供給する汚水ア使用ｊることができ、汚水ケ使用す
るときは汚水ン反応槽／に注ステｂポンプの圧カン利用
できるので、別にポンプ７使用する必要がなく好都合で
ある。The pressure water can be treated water discharged from the drain pipe 7 or sewage water supplied to the reaction tank through the supply pipe 6. This is advantageous because there is no need to use a separate pump 7.
そして１．サイクロンから移送槽１０に生物担体粒子ン
流下させ定ら弁Ｖｚ、Ｖｇ’に閉、弁Ｖ、ン開にし次回
にサイクロンで剥離するための生物担体粒子をサイクロ
ンに入ｎろ。And 1. Let the biological carrier particles flow down from the cyclone to the transfer tank 10, close the valves Vz and Vg', open the valves V, and then introduce the biological carrier particles to the cyclone for next time peeling with the cyclone.
尚、図中ノコは途中に開閉弁ｙ、／ ｙ有し、移送槽１
０の密閉された内部ンサイクロンｑの上部に通じさせる
配管で、サイクロンから生物担体粒子乞移送槽１０に流
下させる際に弁Ｖｓ’Ｙ開（。In addition, the saw in the figure has on-off valves y, / y in the middle, and the transfer tank 1
The pipe is connected to the upper part of the sealed internal cyclone q, and the valve Vs'Y is opened when the biological carrier particles are allowed to flow down from the cyclone to the transfer tank 10.
次に液体サイクロン、特に下部が逆円錐形のものが生物
担体粒子に付着する生物膜の剥離に遣することン実験結
果により示す。Next, experimental results show that a hydrocyclone, especially one with an inverted conical lower part, can be used to peel off biofilms attached to biocarrier particles.
グルコース、酢酸の混合合成基質欠円い、負荷’ｆ（１
０Ｋ？ −ＣＯＤ ｃｒ ／ｖ１．ｄで、生物膜厚ｔＩ
Ｉ）〜６０μｆｉ％［径θ２．のゼオライトの剥離速度
χ測定した。A mixed synthetic substrate of glucose and acetic acid, the load 'f(1
0K? -COD cr /v1. d, biofilm thickness tI
I) ~60μfi% [diameter θ2. The exfoliation rate χ of zeolite was measured.
実験用液体サイクロンの容器は下部の逆円錐形の頂角ｔ
ｔｏ０、円錐底部の直径ｔＯＷ、円筒部の直径１００
調、容量へＳｔである。生物担体粒子を容器内に’ｌ０
０ｍ１投入し、全量を八よｔ とした後、ポンプで容器
上部の液ン円筒部に接線方向に注入し、循環させた。The experimental hydrocyclone container has an inverted conical shape at the bottom with an apex angle t
to0, diameter of the conical bottom tOW, diameter of the cylindrical part 100
The key is St to the capacity. Place the biocarrier particles into the container.
After adding 0ml of the liquid to bring the total volume to 80t, the liquid was injected tangentially into the cylindrical part at the top of the container using a pump and circulated.
ポンプの運転条件はＳＶ （循環水量）ｒｏ−１ｔθ／
／ｈｒ、 で、円錐底部でのＬＶ （通水線速度）は、
？Ｊ〜／／、５ｍ／ｈｒである。評時間ポンプ？運転し
たあとの剥離状態は次の通りである。The pump operating conditions are SV (circulated water volume) ro-1tθ/
/hr, and the LV (linear velocity of water flow) at the bottom of the cone is
? J~//, 5m/hr. Review time pump? The state of peeling after operation is as follows.
ＳＶ ＬＶ 剥離量
！ｒＯ／／ｈｒ 、３．１ｍ７’ｈｒ
Ｏ，Ｏｂ／ ｇｖｓｅ／ｇ−ｖｓｓ、ｄｌｏｏ
＃ ７．ｌｓｌ Ｏ，０７ｇ
Ｉ／！０１／八ｊ’ ０．／！ １比較
のために直径１００ 、容量へ５ｔの容器ン用い、ポン
プの運転条件’Ｉ’ ｇｖ／ ００ 、 ／！ｒＯ／／
ｈｒ （ＬＶ７Ｊ、／／、ｈ＾デ）で同量の同じ生物担
体粒子の剥離χ行った結果は次の通りである。SV LV Peeling amount! rO//hr, 3.1m7'hr
O, Ob/ gvse/g-vss, dloo
#7. lsl O, 07g
I/! 01/8j' 0. /! 1. For comparison, a container with a diameter of 100 mm and a capacity of 5 tons is used, and the pump operating conditions are 'I' gv/00, /! rO//
The same amount of the same biological carrier particles was exfoliated using hr (LV7J, //, h^de) and the results are as follows.
ＳＶ ＬＶ 剥離量
１００ り−ｂ ｏ、ｏ
ｏｇ／！０ ／／、！ ０
．０／／１１どの場合も担体粒子の粉砕は生じなかった
。SV LV Peeling amount 100 Ri-b o, o
og/! 0 //,! 0
．． 0//11 No crushing of the carrier particles occurred in any case.
しかし、上記両結果で判る様に下部が逆円錐形の液体サ
イクロンによｎば同じＳＶで剥離量は７０〜／３倍にも
達した。However, as can be seen from the above results, when using a hydrocyclone with an inverted conical lower part, the amount of peeling reached 70 to 3 times as much at the same SV.
（発明の効果）
本発明によｎば流動床式反応槽の運転中、生物膜が過剰
に厚く付着した生物担体粒子ン反応槽から液体サイクロ
ンに抜出し、こ−で粒子ケ粉砕することなく付着した膜
厚乞所要の薄さに調整し、反応槽に返送する。(Effects of the Invention) According to the present invention, during operation of a fluidized bed reactor, biological carrier particles to which an excessively thick biofilm has adhered are extracted from the reactor to a liquid cyclone, thereby allowing the particles to adhere without being crushed. Adjust the film thickness to the required thickness and return it to the reaction tank.
こｎにより流動床を構成する生物担体粒子の見掛は比重
は均一化し、均一な流動状態で運転欠継続できる。そし
て、高負荷（’ １０ Ｋｑ−ＣＯＤｃｒ／ｒｒ？、ｄ
以上）でも処理が可能になり、担体粒子の補充は不要な
のでランニングコストも低減する。As a result, the apparent specific gravity of the biological carrier particles constituting the fluidized bed becomes uniform, and operation interruptions can be continued in a uniform fluidized state. And high load (' 10 Kq-CODcr/rr?, d
(above) can be processed, and since there is no need to replenish carrier particles, running costs are also reduced.
尚、図示の実施例は嫌気式処理の反応槽であるが、好気
式処理の反応槽にもそのま又実施できることは言う迄も
ない。Although the illustrated embodiment is a reaction tank for anaerobic treatment, it goes without saying that the present invention can also be applied to a reaction tank for aerobic treatment.
図面は本発明の一実施例χ示す系統図で、図中、／は反
応槽、コは流動床、−′はその上部界面、３は抜出手段
、ｑは液体サイクロン、３は返送手段欠示す。The drawing is a system diagram showing one embodiment of the present invention. show.
Claims (1)
動床式反応槽と、該反応槽の流動床界面付近に開口した
生物担体粒子の抜出手段と、該抜出手段から出る生物担
体粒子を受入れる下部が逆円錐形の液体サイクロンと、
該液体サイクロンから担体粒子を前記流動床式反応槽に
返送する返送手段とを有することを特徴とする汚水処理
装置。A fluidized bed reaction tank containing biological carrier particles and biochemically treating wastewater; a means for extracting the biological carrier particles opened near the fluidized bed interface of the reaction tank; and a biological carrier coming out of the extracting means. A hydrocyclone with an inverted conical bottom that receives particles;
A sewage treatment apparatus comprising a return means for returning carrier particles from the liquid cyclone to the fluidized bed reaction tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60219054A JPS6279896A (en) | 1985-10-03 | 1985-10-03 | Sewage treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP60219054A JPS6279896A (en) | 1985-10-03 | 1985-10-03 | Sewage treatment device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS6279896A true JPS6279896A (en) | 1987-04-13 |
Family
ID=16729540
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP60219054A Pending JPS6279896A (en) | 1985-10-03 | 1985-10-03 | Sewage treatment device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS6279896A (en) |
Cited By (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1992009533A1 (en) * | 1990-11-21 | 1992-06-11 | Isamu Iwai | Sewage purifying device of filter material circulation type |
| US5372712A (en) * | 1993-02-25 | 1994-12-13 | Envirex Inc. | Biomass growth control apparatus for fluid bed biological reactor |
| US5387335A (en) * | 1990-11-21 | 1995-02-07 | Iwai; Isamu | Filter circulating type sewage disposal apparatus |
| US5429740A (en) * | 1991-07-03 | 1995-07-04 | Patent Care Bv | Device for the purification of waste water |
| JPH0771673B1 (en) * | 1990-11-21 | 1995-08-02 | ||
| US5494574A (en) * | 1994-08-09 | 1996-02-27 | Envirogen, Inc. | Mechanically mixed packed bed bioreactor |
| WO1998008586A1 (en) * | 1996-08-26 | 1998-03-05 | Bio-Con Labs | Fluidized bed filter |
| KR19980033651A (en) * | 1998-05-06 | 1998-07-25 | 이상을 | Sand microbial contact abatement method |
| JP2003080284A (en) * | 2001-09-14 | 2003-03-18 | Sumitomo Heavy Ind Ltd | Wastewater treatment equipment |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60139394A (en) * | 1983-12-27 | 1985-07-24 | Osaka Gas Co Ltd | Biological treatment of waste water by employing fluidized bed |
-
1985
- 1985-10-03 JP JP60219054A patent/JPS6279896A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS60139394A (en) * | 1983-12-27 | 1985-07-24 | Osaka Gas Co Ltd | Biological treatment of waste water by employing fluidized bed |
Cited By (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO1992009533A1 (en) * | 1990-11-21 | 1992-06-11 | Isamu Iwai | Sewage purifying device of filter material circulation type |
| US5387335A (en) * | 1990-11-21 | 1995-02-07 | Iwai; Isamu | Filter circulating type sewage disposal apparatus |
| JPH0771673B1 (en) * | 1990-11-21 | 1995-08-02 | ||
| US5429740A (en) * | 1991-07-03 | 1995-07-04 | Patent Care Bv | Device for the purification of waste water |
| US5372712A (en) * | 1993-02-25 | 1994-12-13 | Envirex Inc. | Biomass growth control apparatus for fluid bed biological reactor |
| US5976365A (en) * | 1993-02-25 | 1999-11-02 | Envirex, Inc. | Biomass growth control apparatus for fluid bed biological reactor |
| US5494574A (en) * | 1994-08-09 | 1996-02-27 | Envirogen, Inc. | Mechanically mixed packed bed bioreactor |
| WO1998008586A1 (en) * | 1996-08-26 | 1998-03-05 | Bio-Con Labs | Fluidized bed filter |
| KR19980033651A (en) * | 1998-05-06 | 1998-07-25 | 이상을 | Sand microbial contact abatement method |
| JP2003080284A (en) * | 2001-09-14 | 2003-03-18 | Sumitomo Heavy Ind Ltd | Wastewater treatment equipment |
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