JPH0734917B2 - Aerobic digestion concentrator - Google Patents
Aerobic digestion concentratorInfo
- Publication number
- JPH0734917B2 JPH0734917B2 JP1351589A JP1351589A JPH0734917B2 JP H0734917 B2 JPH0734917 B2 JP H0734917B2 JP 1351589 A JP1351589 A JP 1351589A JP 1351589 A JP1351589 A JP 1351589A JP H0734917 B2 JPH0734917 B2 JP H0734917B2
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- flow path
- reaction tank
- digestion
- reaction
- 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.)
- Expired - Lifetime
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
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
- Treatment Of Sludge (AREA)
Description
【発明の詳細な説明】 （産業上の利用分野） 本発明は、下水汚泥の濃縮と好気性消化を単一設備で行
わせるようにした装置に関するものである。TECHNICAL FIELD The present invention relates to a device for concentrating sewage sludge and performing aerobic digestion in a single facility.
（従来の技術） 水処理過程で発生する汚泥の処理は、一般に、濃縮、消
化、脱水、乾燥等の各工程を経て行われている。このう
ち、濃縮処理には従来重力濃縮法、加圧浮上法、遠心濃
縮法が多く用いられている。また、消化処理には嫌気性
消化法と好気性消化法との二つがある。嫌気性消化処理
ではメタンガスを発生するので、エネルギーを回収し後
処理に利用できるという特徴があり、これまで消化処理
の主力をなしてきた。これに対し好気性消化処理は、嫌
気性消化に比べて維持管理が容易であり、臭気を発生し
ないということから、処理場の敷地面積が小さい小規模
施設にとって有利なものとして採用されている。(Prior Art) Treatment of sludge generated in a water treatment process is generally carried out through steps such as concentration, digestion, dehydration, and drying. Among them, the gravity concentration method, the pressure flotation method, and the centrifugal concentration method have been widely used for the concentration treatment. Further, there are two digestive treatments, an anaerobic digestion method and an aerobic digestion method. Since methane gas is generated during anaerobic digestion, it has the characteristic of being able to recover energy and use it for post-treatment, and it has been the mainstay of digestion treatment so far. On the other hand, aerobic digestion is easier to maintain and manage than anaerobic digestion and does not generate odor, so it has been adopted as an advantage for small-scale facilities with a small site area of the treatment plant.
（発明が解決しようとする課題） ところで、濃縮と消化は汚泥処理の前半の工程として重
要なものとなっているが、採用されている濃縮処理のう
ち重力濃縮は最も簡単であるが濃縮性が悪く大型のもの
となるため、加圧浮上や遠心濃縮の採用が増えている
が、それらはコストが高くなるという難点がある。いず
れにしても上記従来の濃縮法では、固形物回収率は70〜
90％程度である。(Problems to be solved by the invention) By the way, although concentration and digestion are important as the first half step of sludge treatment, gravity concentration is the simplest of the concentration treatments used, but the concentration property is Since it becomes a bad and large size, the use of pressure levitation and centrifugal concentration is increasing, but they have a drawback of high cost. In any case, in the above conventional concentration method, the solid recovery rate is 70-
It is about 90%.
また、消化処理のうち好気性消化についてみると、この
方法では空気（酸素）の吹込みが不可欠であるため、嫌
気性消化に比べて動力費が高くつくという欠点がある。In addition, regarding aerobic digestion among digestive treatments, since this method requires blowing air (oxygen), it has a drawback that power cost is higher than that of anaerobic digestion.
また、従来の好気性消化は水深４〜5mの反応槽で処理し
ており、酸素の溶解効率が低く送風量が多くなる欠点を
有している。Further, conventional aerobic digestion is carried out in a reaction tank having a water depth of 4 to 5 m, which has a drawback that oxygen dissolution efficiency is low and the amount of air blown is large.
さらに好気性消化に当ってその反応温度は30〜50℃の中
温域が有利であることが知られているが、従来は反応温
度は外気温に影響されることが多く、温度を上昇させる
には加温設備を別途設けるか純酸素を吹込んで放熱量を
抑える等の工夫が必要である。Furthermore, it is known that the reaction temperature for aerobic digestion is preferably in the medium temperature range of 30 to 50 ° C, but in the past, the reaction temperature was often affected by the outside temperature, and it was difficult to raise the temperature. It is necessary to install additional heating equipment or to inject pure oxygen to suppress the amount of heat released.
本発明は、上記のような実状にかんがみなされたもの
で、濃縮の固液分離での固形物回収率を上げると共に、
分解速度の速い好気性処理を与えるようにし、しかも、
従来格別の設備で行なっていた濃縮と好気性処理を単一
の設備で行えるようにして、小規模の施設で能率よく汚
泥処理することができ、運転管理及び運転経費が少なく
てすむ、汚泥の濃縮と消化とを同時に行う新規な装置を
提供しようとするものである。The present invention, which has been considered to be the actual situation as described above, increases the solids recovery rate in the solid-liquid separation of concentration, and
It gives aerobic treatment with a fast decomposition rate, and
By enabling concentration and aerobic treatment to be performed in a single facility, which was conventionally done in a special facility, sludge can be efficiently treated in a small-scale facility, and operation management and operating costs can be reduced. The present invention aims to provide a new device that simultaneously performs concentration and digestion.
（課題を解決するための手段） 上記の目的を達成するための本発明の構成について実施
例に対応する図面を参照して説明すると、本発明は、上
下に長い下降流路４とこれに続く上昇流路５を設けると
共に上昇流路５中に空気を送入する給気装置７を設け
て、汚泥の好気性消化を行う反応槽１を形成し、この反
応槽１の上部の上昇流路５中に、限外ろ過膜10を設置す
ると共に、限外ろ過膜10より流出する分離液及び反応槽
より排出される消化汚泥によって、反応槽１に供給され
る原汚泥を加温するための熱交換器18,19を設けたこと
を特徴とするものである。(Means for Solving the Problems) The structure of the present invention for achieving the above object will be described with reference to the drawings corresponding to the embodiments. The reaction chamber 1 for aerobic digestion of sludge is formed by providing the ascending flow path 5 and the air supply device 7 for feeding air into the ascending flow path 5, and the ascending flow path above this reaction tank 1. In order to heat the raw sludge supplied to the reaction tank 1 by installing the ultrafiltration membrane 10 in 5 and by the separated liquid flowing out from the ultrafiltration membrane 10 and the digested sludge discharged from the reaction tank. The heat exchangers 18 and 19 are provided.
（実施例） 以下、本発明の実施例について図面を参照して説明す
る。(Example) Hereinafter, the Example of this invention is described with reference to drawings.
図において１は汚泥の消化処理を行う深層曝気槽型の反
応槽で、上下に長く形成した大径の外筒２内に、上下に
長く形成した小径の内筒３がその下端を外筒２の底板よ
り間隔をおいて配置され、内筒３には原汚泥の下降流路
４が、また、内筒２と外筒１との間には上昇流路５が形
成されている。そして、上昇流路の中間部には送気ポン
プ（コンプレッサー）６に連通した給気装置7,7が設け
られており、給気装置７より空気を吹込むことによっ
て、エアリフトにより槽内の汚泥は下降流路４と上昇流
路とを循環すると共に好気性消化処理を受けることにな
る。また、上昇流路５の上部には、槽１に隣接して設け
た消化汚泥貯槽９に開口する消化汚泥排出管８が接続さ
れ、さらにその上部の上昇流路５内には、セラミック性
の限外ろ過膜のモジュール10,10が設置されている。こ
の限外ろ過膜のモジュール10は、従来知られているよう
に、セラミック性の管型ろ過膜を集合させたもので、各
モジュール10よりの分離液は分離液排出管路11に設けた
吸引ポンプ12によって管路11に集められ、分離液貯槽13
に流入されるようになっている。そして、この限外ろ過
膜モジュール10は、給気装置７から吹込まれる空気によ
り、その膜面は常時洗浄されており、高いフラックスを
維持できるようになっている。In the figure, reference numeral 1 is a deep aeration tank type reaction tank for digesting sludge, and a large diameter outer cylinder 2 vertically elongated is provided with a small diameter inner cylinder 3 vertically elongated at its lower end to an outer cylinder 2 Is arranged at a distance from the bottom plate of the above, and a descending channel 4 for raw sludge is formed in the inner cylinder 3, and an ascending channel 5 is formed between the inner cylinder 2 and the outer cylinder 1. In the middle of the ascending flow path, there are provided air supply devices 7, 7 communicating with an air supply pump (compressor) 6. By blowing air from the air supply device 7, sludge in the tank is lifted by an air lift. Circulates through the descending flow path 4 and the ascending flow path and undergoes aerobic digestion processing. Further, a digested sludge discharge pipe 8 opening to a digested sludge storage tank 9 provided adjacent to the tank 1 is connected to the upper part of the ascending flow path 5, and a ceramic material is further provided in the ascending flow path 5 above the digested sludge discharge pipe 8. Ultrafiltration membrane modules 10, 10 are installed. As is conventionally known, the module 10 of the ultrafiltration membrane is a collection of ceramic tubular filtration membranes, and the separation liquid from each module 10 is suctioned in the separation liquid discharge pipe line 11. It is collected in the pipe line 11 by the pump 12, and the separated liquid storage tank 13
It is supposed to be flown into. The membrane surface of the ultrafiltration membrane module 10 is constantly cleaned by the air blown from the air supply device 7, and a high flux can be maintained.
消化汚泥貯槽９に貯留された消化汚泥は、送泥ポンプ14
により汚泥移送管15を通って後続の汚泥処理設備（図示
を略す）に移送され、また、脱離液貯槽に入った分離液
は、送水ポンプ16により送水管17を通って水処理設備
（図示を略す）に送られるが、それらの消化汚泥及び分
離液は、汚泥の分解発酵熱により約35℃の温度を有して
いるので、それぞれ熱交換器18,19を経て放熱するよう
にしてある。そして、水処理設備より原汚泥貯槽20に入
った原汚泥は、上記の熱交換器19,18に接続した管路21
にポンプ22により送られて予備加温が施された後、反応
槽１の上部に供給されるようになっているのである。The digested sludge stored in the digested sludge storage tank 9 is sent by the mud pump 14
Is transferred to the subsequent sludge treatment facility (not shown) through the sludge transfer pipe 15, and the separated liquid that has entered the desorption liquid storage tank is passed through the water pipe 17 by the water pump 16 to the water treatment facility (not shown). The digested sludge and the separated liquid have a temperature of about 35 ° C due to the heat of decomposition and fermentation of the sludge, so that they are radiated through the heat exchangers 18 and 19, respectively. . Then, the raw sludge that has entered the raw sludge storage tank 20 from the water treatment facility is pipe 21 connected to the heat exchangers 19 and 18 described above.
It is sent to the upper part of the reaction tank 1 after being sent by the pump 22 to be preheated.
上記のように、原汚泥貯槽１より送られる原汚泥は、熱
交換器19,18により予備加温されることにより、常温で
ある15〜20℃から、反応（分解）速度の大きい30〜50℃
の中温域内の温度に加温されて反応槽１に供給される。
反応槽１に入った原汚泥は、給気装置7,7から送入され
る空気のエアリフト作用で、下降流路４から上昇流路５
へと矢印のように流動して反応槽１内を循環することに
なりその間汚泥は空気（酸素）の供給を受けて消化さ
れ、固形物の20〜30％が分解し、減量化＜安定化してい
くことになる。そして、反応槽１内の循環汚泥は限外ろ
過膜のモヂュール10,10を通ってろ過され、ろ過された
分離液は吸引ポンプ12の作用で管路11より分離液貯槽13
に流入することになり、処理（消化）された汚泥は排出
管８より外部の消化汚泥貯槽９に排出されることにな
る。そして、反応槽１より排出される分離液及び消化汚
泥は、汚泥自身の分解熱によって約35℃の温度となって
いるので、その廃熱を熱交換器18,19によって反応槽１
への供給原汚泥の加温に有効に利用することになる。As described above, the raw sludge sent from the raw sludge storage tank 1 is preheated by the heat exchangers 19 and 18, so that the reaction (decomposition) rate is high at 30 to 50 from the normal temperature of 15 to 20 ° C. ℃
It is heated to a temperature in the medium temperature range and is supplied to the reaction tank 1.
The raw sludge that has entered the reaction tank 1 is moved from the descending flow path 4 to the ascending flow path 5 by the air lift action of the air sent from the air supply devices 7, 7.
The sludge flows as shown by the arrow and circulates in the reaction tank 1. During that time, the sludge is digested by the supply of air (oxygen), 20 to 30% of the solid matter is decomposed, and the weight reduction <stabilization I will go. Then, the circulating sludge in the reaction tank 1 is filtered through the modules 10, 10 of the ultrafiltration membrane, and the filtered separated liquid is operated by the suction pump 12 from the pipe line 11 to the separated liquid storage tank 13
The treated (digested) sludge is discharged to the outside digested sludge storage tank 9 through the discharge pipe 8. Since the separated liquid and the digested sludge discharged from the reaction tank 1 have a temperature of about 35 ° C. due to the decomposition heat of the sludge itself, the waste heat thereof is removed by the heat exchangers 18 and 19.
It will be effectively used for heating raw sludge.
次に、上記実施例による装置の設計、試算例について説
明すると次のとおりである。Next, the design and trial calculation example of the device according to the above embodiment will be described as follows.
（１）条件 汚水量 50,000m3/日の下水処理場 汚泥発生量 6750kg−ds/日 濃度 1.5％ 汚泥量 450m3/日 （２）反応槽（消化槽） 形状 外筒3500φ×50,000H 内筒1200φ 容量 有効 450m3×２基、滞溜日数２日 （３）限外ろ過膜 形式 チューブ式無機膜 膜面積 170m2/基×２基 （４）送風機 コンプレッサー 6.5m3/分×37kw×２台 （５）分離液吸引ポンプ 0.4m3/分×2.2kw×２台 （６）熱交換器 35m2×２台、30m2×２台 （７）性能 投入汚泥 450m3/日、VS75％、濃度 1.5％ 消化反応 VS分解率25％ 反応温度35℃ 濃縮汚泥 183m3/日、濃度3.0％、VS69％ 分離液 267m3/日 SS 0mg/（固形回収率100％） （発明の効果） 以上説明したように、本発明の装置は、上下に長い下降
流路とこれに続く上昇流路を設けると共に上昇流路中に
空気を送入する給気装置を設けて、汚泥の好気性消化を
行う反応槽を形成し、この反応槽の上部の上昇流路中
に、限外ろ過膜を設置すると共に、限外ろ過膜より流出
する分離液及び反応槽より排出される消化汚泥によっ
て、反応槽に供給される原汚泥を加温するための熱交換
器を設けた構成としたので、次のような優れた効果を奏
するものである。(1) Conditions Sewage treatment amount 50,000m 3 / day Sewage treatment plant Sludge generation amount 6750kg-ds / day Concentration 1.5% Sludge amount 450m 3 / day (2) Reaction tank (digestion tank) Shape Outer cylinder 3500φ × 50,000H Inner cylinder 1200φ capacity Effective 450m 3 × 2 units, retention days 2 days (3) Ultrafiltration membrane type Tube type inorganic membrane Membrane area 170m 2 / unit × 2 units (4) Blower compressor 6.5m 3 / min × 37kw × 2 units (5) Separated liquid suction pump 0.4m 3 / min × 2.2kw × 2 units (6) Heat exchanger 35m 2 × 2 units, 30m 2 × 2 units (7) Performance input sludge 450m 3 / day, VS 75%, concentration 1.5% digestion reaction VS decomposition rate of 25% the reaction temperature 35 ° C. concentrated sludge 183m 3 / day, a concentration of 3.0%, was described VS69% separated liquid 267m 3 / day SS 0 mg / (solid 100% recovery) (effect of the invention) or As described above, the device of the present invention is provided with a vertically long descending flow path and an ascending flow path following the descending flow path and an air supply device for feeding air into the ascending flow path to perform aerobic digestion of sludge. A reaction vessel is formed, and an ultrafiltration membrane is installed in the ascending flow path at the top of this reaction vessel, and the separated solution flowing out from the ultrafiltration membrane and the digested sludge discharged from the reaction vessel causes the reaction vessel to enter the reaction vessel. Since the heat exchanger for heating the supplied raw sludge is provided, it has the following excellent effects.
（１）好気性消化槽（反応槽）を深槽曝気型としてエア
リフトにより汚泥を循環させるようにしたので、酸素の
溶解効率が良好となり省エネ化が図れる。また、不必要
な空気の投入が防がれ反応槽内の温度低下を防ぐことが
できるため、反応槽内の好気性消化に有利な中温域に維
持できる。また、酸素の供給と同時にろ過膜の洗浄がで
き、さらに、生物反応、循環攪拌、濃縮の３作用が単一
の設備と動力源で行ない得られ、施設の場所と経費とが
大巾に低減できる。(1) Since the aerobic digestion tank (reaction tank) is a deep tank aeration type and the sludge is circulated by the air lift, the oxygen dissolution efficiency is improved and energy saving can be achieved. In addition, since unnecessary introduction of air can be prevented and the temperature in the reaction tank can be prevented from lowering, the temperature in the reaction tank can be maintained in an intermediate temperature range that is advantageous for aerobic digestion. In addition, the filtration membrane can be washed simultaneously with the supply of oxygen, and the biological reaction, circulation stirring, and concentration can be performed by a single facility and power source, greatly reducing the location and cost of the facility. it can.
（２）反応槽の上部に限界ろ過膜のモジュールを設置し
たので、限外ろ過膜により分離液のSSは０となり、水処
理への返流水負荷は大巾に軽減できる。また、系外に返
流水として汚泥を出さないため、処理に有用な微生物
を、反応槽内に高濃度に保持でき、また汚泥の滞留時間
も長く保てるので、好気性消化反応を効率よく進められ
る。(2) Since the ultrafiltration membrane module is installed on the upper part of the reaction tank, the SS of the separated liquid becomes 0 due to the ultrafiltration membrane, and the return water load to the water treatment can be greatly reduced. In addition, since sludge is not discharged as return water outside the system, microorganisms useful for treatment can be kept in a high concentration in the reaction tank, and the retention time of sludge can be maintained for a long time, so aerobic digestion reaction can proceed efficiently. .
（３）原汚泥は深層曝気の反応槽内を循環するので消化
処理が効率よくでき、固形物の20〜30％が分解されて減
量化、安定化するので、脱水以降の処理が容易になる。(3) The raw sludge circulates in the deep aeration reaction tank so that it can be efficiently digested, and 20 to 30% of the solid matter is decomposed to reduce and stabilize the solid sludge, which facilitates the treatment after dehydration. .
（４）原汚泥は、消化汚泥及び分離液と熱交換器を通し
て予備加温されて反応槽に入るので、反応（分解）速度
が大になると共に、系外に排出される消化汚泥及び分離
液の廃熱を回収して有効利用が図れることになる。(4) The raw sludge is preheated through the heat exchanger with the digested sludge and the separated liquid, and enters the reaction tank, so that the reaction (decomposition) speed increases and the digested sludge and the separated liquid discharged to the outside of the system. The waste heat of will be recovered and can be effectively used.
図面は本発明の一実施例を示す形態の説明図である。 １……反応槽、２……外筒、３……内筒 ４……下降流路、５……上昇流路 ７……給気送置、８……消化汚泥排出管 ９……消化汚泥貯槽 10……限外ろ過膜のモジュール 11……分離液排出管、13……分離液貯槽 18,19……熱交換器 20……原汚泥貯槽、21……管路 The drawings are explanatory views of a mode showing an embodiment of the present invention. 1 ... Reaction tank, 2 ... Outer cylinder, 3 ... Inner cylinder, 4 ... Downward flow path, 5 ... Upflow path, 7 ... Air supply, 8 ... Digested sludge discharge pipe, 9 ... Digested sludge Storage tank 10 …… Module for ultrafiltration membrane 11 …… Separation liquid discharge pipe, 13 …… Separation liquid storage tank 18, 19 …… Heat exchanger 20 …… Raw sludge storage tank, 21 …… Pipe line
Claims (1)
を設けると共に上昇流路中に空気を送入する給気装置を
設けて、汚泥の好気性消化を行う反応槽を形成し、この
反応槽の上部の上昇流路中に、限外ろ過膜を設置すると
共に、限外ろ過膜より流出する分離駅及び反応槽より排
出される消化汚泥によって、反応槽に供給される原汚泥
を加温するための熱交換器を設けたことを特徴とする、
好気性消化濃縮装置。1. A reaction tank for aerobic digestion of sludge is formed by providing a vertically long descending flow path and an ascending flow path following the descending flow path and an air supply device for feeding air into the ascending flow path. , An ultrafiltration membrane is installed in the ascending flow path at the top of this reaction tank, and the raw sludge supplied to the reaction tank by the digestion sludge discharged from the separation station and the reaction tank flowing out from the ultrafiltration membrane. A heat exchanger for heating the
Aerobic digestion concentrator.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1351589A JPH0734917B2 (en) | 1989-01-23 | 1989-01-23 | Aerobic digestion concentrator |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1351589A JPH0734917B2 (en) | 1989-01-23 | 1989-01-23 | Aerobic digestion concentrator |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02194899A JPH02194899A (en) | 1990-08-01 |
| JPH0734917B2 true JPH0734917B2 (en) | 1995-04-19 |
Family
ID=11835288
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1351589A Expired - Lifetime JPH0734917B2 (en) | 1989-01-23 | 1989-01-23 | Aerobic digestion concentrator |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0734917B2 (en) |
Families Citing this family (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH0818032B2 (en) * | 1990-11-30 | 1996-02-28 | 株式会社荏原製作所 | Solid-liquid separation integrated biological treatment method and biological treatment apparatus |
| JPH04300693A (en) * | 1991-03-29 | 1992-10-23 | Kubota Corp | Water treatment apparatus |
| EP4733273A2 (en) | 2013-02-22 | 2026-04-29 | BL Technologies, Inc. | Membrane assembly for supporting a biofilm |
| CA3207201A1 (en) | 2014-03-20 | 2015-09-24 | Bl Technologies, Inc. | Wastewater treatment with primary treatment and mbr or mabr-ifas reactor |
-
1989
- 1989-01-23 JP JP1351589A patent/JPH0734917B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPH02194899A (en) | 1990-08-01 |
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