JPH01236995A - Deep structure waste water treating method - Google Patents
Deep structure waste water treating methodInfo
- Publication number
- JPH01236995A JPH01236995A JP62264702A JP26470287A JPH01236995A JP H01236995 A JPH01236995 A JP H01236995A JP 62264702 A JP62264702 A JP 62264702A JP 26470287 A JP26470287 A JP 26470287A JP H01236995 A JPH01236995 A JP H01236995A
- Authority
- JP
- Japan
- Prior art keywords
- less
- tank
- waste water
- carrier particles
- water treating
- 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
- 238000000034 method Methods 0.000 title claims abstract description 21
- 239000002351 wastewater Substances 0.000 title claims abstract description 17
- 239000002245 particle Substances 0.000 claims abstract description 48
- 239000010802 sludge Substances 0.000 claims abstract description 24
- 239000007788 liquid Substances 0.000 claims abstract description 17
- 239000007789 gas Substances 0.000 claims abstract description 13
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims abstract description 11
- 239000001301 oxygen Substances 0.000 claims abstract description 11
- 229910052760 oxygen Inorganic materials 0.000 claims abstract description 11
- 230000005484 gravity Effects 0.000 claims abstract description 10
- 230000000813 microbial effect Effects 0.000 claims description 5
- 238000004065 wastewater treatment Methods 0.000 claims description 3
- 244000005700 microbiome Species 0.000 abstract description 3
- 238000005422 blasting Methods 0.000 abstract 1
- 238000000926 separation method Methods 0.000 description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 5
- 238000005273 aeration Methods 0.000 description 4
- 238000007664 blowing Methods 0.000 description 4
- 230000000694 effects Effects 0.000 description 4
- 230000007423 decrease Effects 0.000 description 2
- 238000005516 engineering process Methods 0.000 description 2
- 230000014759 maintenance of location Effects 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 1
- 241000233866 Fungi Species 0.000 description 1
- 239000004743 Polypropylene Substances 0.000 description 1
- 239000000919 ceramic Substances 0.000 description 1
- 230000000052 comparative effect Effects 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 239000010840 domestic wastewater Substances 0.000 description 1
- 238000010304 firing Methods 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910010272 inorganic material Inorganic materials 0.000 description 1
- 239000011147 inorganic material Substances 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 239000005332 obsidian Substances 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 239000004033 plastic Substances 0.000 description 1
- -1 polypropylene Polymers 0.000 description 1
- 229920001155 polypropylene Polymers 0.000 description 1
- 239000011347 resin Substances 0.000 description 1
- 229920005989 resin Polymers 0.000 description 1
- 239000011435 rock Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 239000000126 substance Substances 0.000 description 1
- 239000002023 wood Substances 0.000 description 1
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
本発明は、担体に付着した微生物を使用して、深層処理
槽により、各種のＢＯＤ成分を含有する廃水（都市下水
：生活廃水二食品工場、化学工場、パルプ工場等からの
工場廃水：畜産廃水等）を処理する方法に関する。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention uses microorganisms attached to a carrier to treat wastewater containing various BOD components (urban sewage: domestic wastewater, two food factories, chemical This invention relates to a method for treating industrial wastewater from factories, pulp mills, etc. (livestock wastewater, etc.).
従来の技術とその問題点 深層処理槽による廃水の処理法は、公知である。Conventional technology and its problems Methods for treating wastewater using deep treatment tanks are well known.
例えば、特公昭５９−３８０３１号公報は、いわゆる超
深層曝気法の一例を開示している。この方法によれば、
下水処理設備の所要面積が著るしく減少するとされてい
るが、処理水と活性汚泥とを分離するための大きな沈降
槽を必要とするので、処理装置全体の敷地面積は、それ
程大幅には減少しない。For example, Japanese Patent Publication No. 59-38031 discloses an example of the so-called ultra-deep aeration method. According to this method,
It is said that the area required for sewage treatment equipment will be significantly reduced, but since a large sedimentation tank is required to separate treated water and activated sludge, the site area of the entire treatment equipment will not be reduced that much. do not.
特公昭５７−５９０００号公報に開示された方法では、
上昇流の部分には汚泥に付着した粒子が存在せず、担体
から剥離した汚泥のみが存在するので、汚泥濃度が低く
、処理効率が悪い。また、酸素供給部と酸素消費部とが
分離して居るので、流動層下部まで酸素が十分に供給さ
れない場合があり、処理効率の低下を招く。更に、超深
層曝気方法ではないので、敷地面積も減少しない。In the method disclosed in Japanese Patent Publication No. 57-59000,
In the upward flow section, there are no particles attached to the sludge, and only sludge separated from the carrier is present, so the sludge concentration is low and the treatment efficiency is poor. Furthermore, since the oxygen supply section and the oxygen consumption section are separated, oxygen may not be sufficiently supplied to the lower part of the fluidized bed, resulting in a decrease in processing efficiency. Furthermore, since it is not an ultra-deep aeration method, the site area will not be reduced.
問題点を解決するための手段
本発明者は、上記の如き技術の現状に鑑みて種々研究を
重ねた結果、深層廃水処理法における多数のパラメータ
ーを相互に関連付けて厳格にコントロールすることによ
り、従来技術の問題点を大巾に軽減し得ることを見出だ
した。即ち、本発明は、下記の方法を提供するものであ
る。Means for Solving the Problems As a result of various studies in view of the current state of the technology as described above, the present inventor has determined that a large number of parameters in the deep wastewater treatment method can be interconnected and strictly controlled. We have discovered that the technical problems can be greatly alleviated. That is, the present invention provides the following method.
「下降流部分と上昇流部分とを備えた深層処理槽内で微
生物担体粒子により廃水を処理する方法であって、処理
槽の深さが５０ｍ以上、下降流及び１−昇流の線速か夫
々０．８ｍ／ｓｅｃ以上、担体粒子・の比重が１未満、
担体粒子の粒径が２ｍｍ以下、担体粒子の充填率が２０
〜５０％、下降流への吹き込みガスの酸素ａ麿が８０％
以上、吹き込みガス量（Ｇ）と循環液量（Ｌ）との体積
比（Ｇ／Ｌ）比が０．０５以下、汚泥濃度が１５０００
ｍｇ／ｌ以−ヒの条件を備えたことを特徴とする深層廃
水処理方法。」
以下、図面に示すフローチャートを参照しつつ、本発明
方法を更に詳細に説明する。尚、図面において、・は、
担体粒子を表し、Ｏは、気泡を表すものとする。"A method for treating wastewater with microbial carrier particles in a deep treatment tank equipped with a downward flow section and an upward flow section, the depth of the treatment tank is 50 m or more, and the linear velocity of downward flow and 1-upward flow is 0.8 m/sec or more, the specific gravity of the carrier particles is less than 1, respectively.
The particle size of the carrier particles is 2 mm or less, and the filling rate of the carrier particles is 20
~50%, 80% oxygen in the downflow gas
Above, the volume ratio (G/L) between the amount of blown gas (G) and the amount of circulating liquid (L) is 0.05 or less, and the sludge concentration is 15,000.
A method for treating deep wastewater, characterized in that it has the following conditions: mg/l or more. ” Hereinafter, the method of the present invention will be explained in more detail with reference to the flowchart shown in the drawings. In addition, in the drawing, .
It represents carrier particles and O shall represent air bubbles.
第１図において、深層処理槽（１）は、下降流部分（３
）と上昇流部分（５）とに分画されている。廃水は、ラ
イン（７）を経て深層処理槽（１）に導入され、ライン
（９）から酸素濃度８０％以上の高酸素濃度ガスを吹き
込まれた状態で微生物担体粒子とともに下降流部分（３
）内を下降した後、ライン（１７）を経てエアリフト（
１９）から空気を吹き込まれている上昇流部分（５）内
を上昇する。処理を終えた水の７部は、深層処理槽（１
）を出て、固液分離部（１１）を下降する。通常担体粒
子に付着する汚泥は、槽内の循環流の影響により、一定
の厚さ以上に成長することはないので、固液分離部（１
１）の下降線速が５ｃｍ／ｓｅｃ以下（好ましくは１ｃ
ｍ／ｓｅｃ以下）となるようにすれば、担体粒子は、下
降流に随伴することなくして分離可能である。しかしな
がら、固液分離部の断面積を大きくすることが出来ず、
下降線速が上記の範囲よりも大きくなる場合或いは比重
が比較的１に近い粒子を使用する場合には、粒子に付着
した微生物を固液分離部で何らかの装置又は手段により
剥離すればよい。この場合、例えば、空気吹き込みによ
る激しい撹拌、機械的攪拌、超音波による衝撃等の任意
の剥離方法又は剥離装置（図示せず）により、余剰汚泥
を微生物担体粒子から剥離すれば良い。汚泥を剥離され
た微生物担体粒子は、上昇して、上昇流部分（５）の上
部から再び下降流部分（３）に循環される。一方、固液
分離部（１１）を出た剥離汚泥を含む水は、滞留槽（１
３）を経て、ライン（１５）から系外に取り出される。In Figure 1, the deep treatment tank (1) has a downward flow section (3
) and an upflow part (5). The wastewater is introduced into the deep treatment tank (1) through the line (7), and is passed through the downward flow section (3) together with the microbial carrier particles while being blown with high oxygen concentration gas of 80% or more through the line (9).
), then go through the line (17) to the air lift (
19) in which air is blown into the upflow section (5). Seven parts of the treated water are transferred to a deep treatment tank (1
) and descend through the solid-liquid separation section (11). Normally, the sludge that adheres to the carrier particles does not grow beyond a certain thickness due to the influence of the circulating flow in the tank, so the solid-liquid separation section (1
1) The descending linear velocity is 5 cm/sec or less (preferably 1 c
m/sec or less), carrier particles can be separated without being accompanied by a downward flow. However, it is not possible to increase the cross-sectional area of the solid-liquid separation section,
If the linear velocity of descent is greater than the above range, or if particles with a specific gravity relatively close to 1 are used, microorganisms attached to the particles may be separated by some device or means in the solid-liquid separation section. In this case, the excess sludge may be peeled off from the microbial carrier particles by any peeling method or peeling device (not shown), such as vigorous stirring by air blowing, mechanical stirring, or ultrasonic impact. The microbial carrier particles from which the sludge has been removed rise and are circulated from the upper part of the upflow section (5) to the downflow section (3) again. On the other hand, the water containing the exfoliated sludge that has exited the solid-liquid separation section (11) is transferred to the retention tank (1
3) and is taken out of the system through line (15).
第１図においては、液の循環手段としてエアリフトを示
したが、担体粒子が破損しないかぎり、ポンプ、撹拌機
等の他の公知の手段を採用することができる。In FIG. 1, an air lift is shown as a liquid circulation means, but other known means such as a pump or a stirrer may be used as long as the carrier particles are not damaged.
本発明方法においては、同心円状に配置された内管と外
管とからなる二重円筒を処理槽として使用し、内管内を
下降流部分又は上昇流部分とし、内管と外管この間の空
間（外筒部）を上昇流部分又は下降流部分としても良い
。In the method of the present invention, a double cylinder consisting of an inner tube and an outer tube arranged concentrically is used as a processing tank, the inside of the inner tube is a downward flow section or an upward flow section, and the space between the inner tube and the outer tube is (Outer cylinder part) may be an upflow part or a downflow part.
本発明方法において採用される各種のパラメーターは、
相互に密接に関連しているので、その規定の理由を個々
に説明することは、必ずしも適切であるとはいい難いが
、その理由を示すならば、一応以下の通りである。Various parameters employed in the method of the present invention are:
Since they are closely related to each other, it is not necessarily appropriate to explain the reasons for each provision individually, but the reasons are as follows.
先ず、下降流部分（３）において、比重１未満の担体粒
子とともに廃水を安定して下降させるためには、若干の
余裕をみて、０．８ｍ／ｓｅｃ以ヒの線速を必要とする
。若し、下降流部分（３）への吹き込みガスとして空気
又は比較的酸素濃度の低いガスを使用する場合には、Ｇ
／Ｌ比が太きくなり過ぎて、液の循環抵抗が大きくなり
、気泡か合体して気泡流が形成されない等の問題点を生
じる。従って、下降流部分（３）への吹き込みガスとし
て酸素濃度８０％以上のガスを使用し且つＧ／Ｌ比を０
．０５以下とする。下降流の線速は、１〜２ｍ／ｓｅｃ
程度とし、Ｇ／Ｌ比は、０．０４〜０．００２程度とす
ることがより好ましい。本発明方法では、深層処理槽（
１）内の汚泥濃度を１５０００ｍｇ／９とし、高い負荷
で操作を行うことが可能である。若し、空気からの酸素
を利用して、この様な高い負荷で廃水処理操作を行うと
すれば、液の循環量を増大させなければならない。この
場合、（イ）液深を小さくし且つ処理槽の断面積を大き
くするかまたは（ロ）液の下降流及び上昇流の線速を大
きくすることが考えられる。しかしながら、前者の場合
には、工事費の増大及び循環量の増加に伴う動力費の増
大という問題があり、後者の場合には、線速上昇に必要
な動力費の増大及びエアリフトによる線速増加の限界等
の問題がある。しかるに、本発明では、深層処理槽（１
）の深さを５０ｒｎ以上とし且つ吹き込みガスの酸素濃
度を８０％以上とすることにより、上記の効果を達成し
ている。First, in the downward flow section (3), in order to stably descend the wastewater together with carrier particles having a specific gravity of less than 1, a linear velocity of 0.8 m/sec or more is required with some margin. If air or a gas with relatively low oxygen concentration is used as the blowing gas to the downflow section (3), G
If the /L ratio becomes too large, the circulation resistance of the liquid becomes large, causing problems such as bubbles coalescing and no bubble flow being formed. Therefore, a gas with an oxygen concentration of 80% or more is used as the blowing gas to the downflow section (3), and the G/L ratio is 0.
．． 05 or less. The linear velocity of the downward flow is 1 to 2 m/sec
The G/L ratio is more preferably about 0.04 to 0.002. In the method of the present invention, a deep treatment tank (
1) The sludge concentration in 1) is set to 15000mg/9, making it possible to operate under high load. If wastewater treatment is to be performed under such a high load using oxygen from the air, the amount of liquid circulated must be increased. In this case, it is conceivable to (a) reduce the liquid depth and increase the cross-sectional area of the processing tank, or (b) increase the linear velocity of the downward flow and upward flow of the liquid. However, in the former case, there are problems of increased construction costs and increased power costs due to increased circulation volume, and in the latter case, increased power costs required to increase linear speed and increased linear speed due to airlift. There are problems such as the limits of However, in the present invention, the deep treatment tank (1
) is set to a depth of 50 rn or more and the oxygen concentration of the blown gas is set to 80% or more, thereby achieving the above effect.
本発明方法において、担体粒子の比重を１未満としたの
は、処理槽下部に担体粒子が滞留することを防止すると
ともに、万一、装置が停止した場合にも、再起動を容易
ならしめるためである。又、担体粒子の粒径が２Ｉｌｌ
Ｉ１１以下としたのは、粒子径が大きすぎる場合には、
充填した粒子の占める体積が増加するのに対して表面積
が減少するため、槽内の汚泥濃度を所定の高さに維持で
きなくなるからである。担体粒子は、成長した汚泥が付
着した状態においても、比重が１未満であるものが好ま
しい。より具体的には、例えば、粒径１ｍｍの粒子の場
合には、比重０．６５以下のものが、粒径２ｇ１＋１１
の粒子の場合には、比重０．９以下のものが好ましい。In the method of the present invention, the specific gravity of the carrier particles is set to less than 1 in order to prevent the carrier particles from accumulating at the bottom of the processing tank, and also to facilitate restarting the apparatus in the event that it is stopped. It is. Moreover, the particle size of the carrier particles is 2Ill.
The reason for setting I11 or less is that if the particle size is too large,
This is because while the volume occupied by the filled particles increases, the surface area decreases, making it impossible to maintain the sludge concentration in the tank at a predetermined level. The carrier particles preferably have a specific gravity of less than 1 even when the grown sludge is attached. More specifically, for example, in the case of particles with a particle size of 1 mm, those with a specific gravity of 0.65 or less have a particle size of 2g1+11
In the case of particles, those having a specific gravity of 0.9 or less are preferable.
この様な担体粒子としては、発泡及び非発泡のプラスチ
ック粒子、発泡させた無機材料粒子（例えば、頁岩、黒
曜岩等の岩石を破砕し、焼成して発泡させたものや、シ
ラスバルーン等の発泡セラミクス粒子等）、木材破砕片
等が例示される。Such carrier particles include foamed and non-foamed plastic particles, foamed inorganic material particles (for example, those made by crushing and firing rocks such as shale and obsidian, and foamed ones such as shirasu balloons). (foamed ceramic particles, etc.), crushed wood pieces, etc.
担体粒子の充填率（処理槽中で担体粒子の占める体積の
割合）を２０〜５０％としたのは、２０％未満の場合に
は、担体粒子の使用による効果が十分に発揮されず、一
方、５０％を上回わる場合には、気−液混合相の循環に
多大のエネルギーを必要とするからである。The reason why the filling rate of the carrier particles (the proportion of the volume occupied by the carrier particles in the processing tank) is set to 20 to 50% is because if it is less than 20%, the effect of using the carrier particles will not be sufficiently exhibited. , exceeds 50%, a large amount of energy is required to circulate the gas-liquid mixed phase.
発明の効果 本発明によれば、以下の如き顕著な効果が達成される。Effect of the invention According to the present invention, the following remarkable effects are achieved.
（ａ）処理槽内の活性汚泥濃度を高く維持することがで
き、且つ、汚泥の分離返送を要しない即ち沈降槽が不要
となるので、装置を小形化することができる。(a) The activated sludge concentration in the treatment tank can be maintained high, and there is no need to separate and return the sludge, that is, there is no need for a sedimentation tank, so the apparatus can be downsized.
（ｂ）糸状菌等によるバルキングが発生しても、操作が
妨げられることはない。(b) Even if bulking occurs due to filamentous fungi, operations will not be hindered.
（ｃ）操作が停止した場合にも、担体粒子が処理槽上部
に浮上するので、再起動が容易である。(c) Even if the operation is stopped, the carrier particles float to the top of the processing tank, making restarting easy.
（ｄ）汚泥による目詰まりがなく、粒子の回収も容易で
ある。(d) There is no clogging due to sludge, and particles can be easily collected.
実施例
以下に実施例を示し、本発明の特徴とするところをより
一層明らかにする。EXAMPLES Examples will be shown below to further clarify the features of the present invention.
実施例１
同心円状に配置された内径１８ｃｍの内管と内径２６ｃ
ｍ０外管とからなる長さ１５０ｍの二重円筒からなる深
層処理槽において、内管内を下降流部分とし、内管と外
管との間の空間（外筒部）を上昇流部分とする循環経路
を形成させ、ＢＯＤ６００ｍｇ／９の食品工場排水１６
０ｍ／口を処理した。Example 1 An inner tube with an inner diameter of 18 cm and an inner diameter of 26 cm arranged concentrically
In a deep treatment tank consisting of a double cylinder with a length of 150 m and an outer tube, the inside of the inner tube is the downward flow section, and the space between the inner tube and the outer tube (outer tube section) is the upward flow section. Food factory wastewater with BOD 600mg/9 by forming a channel 16
0m/mouth was treated.
担体粒子としては、処理槽の内容積の３０％に相当する
量の発泡ポリプロピレン樹脂（粒径１．５ｍｍ、比重０
．７）の表面に活性汚泥を予め付着させたものを使用し
た。As the carrier particles, foamed polypropylene resin (particle size 1.5 mm, specific gravity 0
．． 7) was used with activated sludge attached to its surface in advance.
処理液の循環を行うために、外筒部の水深３０ｍのとこ
ろから上昇流に５ｍ’／時間の割合で空気を吹き込んで
エアリフトを形成した。上昇流の線速度は、０．８０ｍ
／ｓｅｃであり、下降流の線速度は、０．８７ｍ／ｓｅ
ｃであった。In order to circulate the treatment liquid, an air lift was formed by blowing air into the upward flow at a rate of 5 m'/hour from a depth of 30 m in the outer cylinder. The linear velocity of the upward flow is 0.80 m
/sec, and the linear velocity of the downward flow is 0.87m/sec.
It was c.
又、内管の水深２０ｍのところから下降流に純酸素２．
５ｒｒ？／時間を吹き込んだ。この時の下降流中のＧ／
Ｌは、０．０３１３であった。In addition, 2.5 g of pure oxygen flows downward from the inner tube at a depth of 20 m.
5rr? / Infused with time. G/ during the downward flow at this time
L was 0.0313.
その結果、担体粒子は、処理槽中を均一に循環しており
、処理槽内の汚泥濃度は、２００００ｍｇ／ｌであった
。従って、ＢＯＤ汚泥負荷は、０．６ｋｇＢＯＤ／ｋｇ
ｓｓ・口で運転が行われた。As a result, the carrier particles were uniformly circulating in the treatment tank, and the sludge concentration in the treatment tank was 20,000 mg/l. Therefore, the BOD sludge load is 0.6 kgBOD/kg
Driving was carried out using SS.
かくして得られた処理水のＢＯＤは、４５ｍｇ／ｌにま
で低下していた。The BOD of the treated water thus obtained was reduced to 45 mg/l.
比較例１
実施例１におけると同様の食品工場廃水を公知の超深槽
曝気方法により実施例１と同様のＢＯＤとなるまで処理
した。Comparative Example 1 The same food factory wastewater as in Example 1 was treated by a known ultra-deep tank aeration method until the same BOD as in Example 1 was obtained.
槽内の汚泥濃度は、５０００ｍｇ／ｌであり、ＢＯＤ汚
泥負荷を０．６ｋｇＢＯＤ／ｋｇｓｓ・日として処理を
行なうためには、直径５２ｃｍｘ長さ１５０ｍの処理槽
が必要であった。また、そのほかに処理槽からの混合液
を脱気処理するための真空脱気塔、脱気済みの混合液を
処理水と返送汚泥とに分離する沈澱槽（直径４．５ｍＸ
高さ４ｍ）、返送汚泥を曝気槽に返送する返送汚泥ポン
プなどの付加的な装置が必要であり、これら装置用の敷
地として５ｍＸ１０ｍの面積が必要であった。The sludge concentration in the tank was 5000 mg/l, and in order to carry out the treatment with a BOD sludge load of 0.6 kgBOD/kgss/day, a treatment tank with a diameter of 52 cm and a length of 150 m was required. In addition, we also have a vacuum deaeration tower for deaerating the mixed liquid from the treatment tank, and a settling tank (diameter 4.5m x
4 m in height), additional equipment such as a return sludge pump to return the returned sludge to the aeration tank was required, and an area of 5 m x 10 m was required as a site for these equipment.
第１図は、本発明の一実施態様を説明するためのフロー
チャートである。
（１）・・・・・・深層処理槽
（３）・・・・・・下降流部分
（５）・・・・・・上昇流部分
（７）・・・・・・廃水供給ライン
（９）・・・・・・高濃度酸素含有ガス供給ライン（１
１）・・・・・・固液分離部
（１３）・・・・・・滞留槽
（１５）・・・・・・処理水取り出しライン（１７）・
・・・・・空気供給ライン
（１９）・・・・・・エアリフト
（以上）
第１図FIG. 1 is a flowchart for explaining one embodiment of the present invention. (1)...Deep treatment tank (3)...Downflow section (5)...Upflow section (7)...Wastewater supply line (9 )...High concentration oxygen-containing gas supply line (1
1) Solid-liquid separation section (13) Retention tank (15) Treated water take-off line (17)
...Air supply line (19) ...Air lift (and above) Figure 1
Claims (1)
で微生物担体粒子により廃水を処理する方法であって、
処理槽の深さが５０ｍ以上、下降流及び上昇流の線速が
夫々０．８ｍ／ｓｅｃ以上、担体粒子の比重が１未満、
担体粒子の粒径が２ｍｍ以下、担体粒子の充填率が２０
〜５０％、下降流への吹き込みガスの酸素濃度が８０％
以上、吹き込みガス量と循環液量との体積比が０．０５
以下、汚泥濃度が１５０００ｍｇ／ｌ以上の条件を備え
たことを特徴とする深層廃水処理法。(1) A method for treating wastewater with microbial carrier particles in a deep treatment tank having a downward flow section and an upward flow section, the method comprising:
The depth of the treatment tank is 50 m or more, the linear velocity of the downward flow and the upward flow are each 0.8 m/sec or more, the specific gravity of the carrier particles is less than 1,
The particle size of the carrier particles is 2 mm or less, and the filling rate of the carrier particles is 20
~50%, oxygen concentration in the downflow gas is 80%
Above, the volume ratio between the amount of blown gas and the amount of circulating liquid is 0.05.
The following is a deep wastewater treatment method characterized by having a sludge concentration of 15,000 mg/l or more.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62264702A JPH01236995A (en) | 1987-10-19 | 1987-10-19 | Deep structure waste water treating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP62264702A JPH01236995A (en) | 1987-10-19 | 1987-10-19 | Deep structure waste water treating method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH01236995A true JPH01236995A (en) | 1989-09-21 |
Family
ID=17406996
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP62264702A Pending JPH01236995A (en) | 1987-10-19 | 1987-10-19 | Deep structure waste water treating method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH01236995A (en) |
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2707183A1 (en) * | 1993-07-06 | 1995-01-13 | Dumez Lyonnaise Eaux | Process for setting in motion microorganism-carrying particles in a liquid to be treated by a biological route and plant for making use of the process |
| JP2009039700A (en) * | 2007-08-13 | 2009-02-26 | Kurita Water Ind Ltd | Wastewater biological treatment method |
-
1987
- 1987-10-19 JP JP62264702A patent/JPH01236995A/en active Pending
Cited By (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| FR2707183A1 (en) * | 1993-07-06 | 1995-01-13 | Dumez Lyonnaise Eaux | Process for setting in motion microorganism-carrying particles in a liquid to be treated by a biological route and plant for making use of the process |
| JP2009039700A (en) * | 2007-08-13 | 2009-02-26 | Kurita Water Ind Ltd | Wastewater biological treatment method |
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