JPS6366597B2 - - Google Patents
Info
- Publication number
- JPS6366597B2 JPS6366597B2 JP10952484A JP10952484A JPS6366597B2 JP S6366597 B2 JPS6366597 B2 JP S6366597B2 JP 10952484 A JP10952484 A JP 10952484A JP 10952484 A JP10952484 A JP 10952484A JP S6366597 B2 JPS6366597 B2 JP S6366597B2
- Authority
- JP
- Japan
- Prior art keywords
- treatment tank
- water level
- treatment
- wastewater
- liquid
- 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
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 67
- 239000010802 sludge Substances 0.000 claims description 42
- 239000007788 liquid Substances 0.000 claims description 36
- 239000002351 wastewater Substances 0.000 claims description 35
- 238000005273 aeration Methods 0.000 claims description 29
- 238000000034 method Methods 0.000 claims description 29
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 8
- 239000001301 oxygen Substances 0.000 claims description 8
- 229910052760 oxygen Inorganic materials 0.000 claims description 8
- 238000007599 discharging Methods 0.000 claims description 3
- 238000003672 processing method Methods 0.000 claims description 2
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 16
- 238000000926 separation method Methods 0.000 description 12
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 9
- 238000001514 detection method Methods 0.000 description 9
- 229910052698 phosphorus Inorganic materials 0.000 description 9
- 239000011574 phosphorus Substances 0.000 description 9
- 229910052757 nitrogen Inorganic materials 0.000 description 8
- 238000010586 diagram Methods 0.000 description 5
- 230000000694 effects Effects 0.000 description 3
- 239000000126 substance Substances 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 239000010840 domestic wastewater Substances 0.000 description 2
- 238000000605 extraction Methods 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- VTEIFHQUZWABDE-UHFFFAOYSA-N 2-(2,5-dimethoxy-4-methylphenyl)-2-methoxyethanamine Chemical compound COC(CN)C1=CC(OC)=C(C)C=C1OC VTEIFHQUZWABDE-UHFFFAOYSA-N 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- -1 ammonia is nitrified Chemical compound 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- FFBHFFJDDLITSX-UHFFFAOYSA-N benzyl N-[2-hydroxy-4-(3-oxomorpholin-4-yl)phenyl]carbamate Chemical compound OC1=C(NC(=O)OCC2=CC=CC=C2)C=CC(=C1)N1CCOCC1=O FFBHFFJDDLITSX-UHFFFAOYSA-N 0.000 description 1
- 238000005056 compaction Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000003344 environmental pollutant Substances 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 238000002955 isolation Methods 0.000 description 1
- 230000007257 malfunction Effects 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 244000005700 microbiome Species 0.000 description 1
- 238000002156 mixing Methods 0.000 description 1
- 231100000719 pollutant Toxicity 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
- 230000008719 thickening Effects 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、各種排水中のBOD、窒素、リンを
生物学的に除去する排水の回分式処理方法に関す
るものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a batch treatment method for wastewater that biologically removes BOD, nitrogen, and phosphorus from various types of wastewater.
排水中のBOD、窒素分の除去は、活性汚泥法
により連続的かつ高率に行われてきたが、活性汚
泥法はバルキングなどを生ずることがあるため
に、管理が比較的難しく、運転要員も多くを必要
としていた。
The removal of BOD and nitrogen from wastewater has been carried out continuously and at a high rate using the activated sludge method, but since the activated sludge method can cause bulking, it is relatively difficult to manage and requires a lot of operating personnel. needed a lot.
一方、回分式に処理する方法では、連続的に処
理するものではないために、比較的大きな貯留槽
を配備しなくてはならず、設備が必要以上に過大
となるといつた欠点があつた。 On the other hand, in the batch treatment method, since the treatment is not continuous, a relatively large storage tank must be provided, which has the disadvantage that the equipment becomes unnecessarily large.
本発明は、前記従来の活性汚泥処理法、回分式
処理法の欠点を解消し、効率のよいBOD除去処
理に加えて窒素、リンの除去機能をも付加し、さ
らに活性汚泥の沈降、濃縮性も大幅に改善できる
回分式処理方法を提供しようとするものである。
The present invention eliminates the drawbacks of the conventional activated sludge treatment method and batch treatment method, adds nitrogen and phosphorus removal functions in addition to efficient BOD removal treatment, and further improves sedimentation and concentration of activated sludge. The aim is to provide a batch processing method that can significantly improve the process.
本発明は、排水が連続して流入し、水位が上下
動しかつ嫌気的雰囲気にある処理槽Ａと、好気的
条件下にある処理槽Ｂを用いて排水を処理するに
際し、処理槽Ａの液を処理槽Ｂに送液して曝気す
るとともにこの送液分の液を処理槽Ｂから処理槽
Ａへ返送し、処理槽Ａの水位が所定水位に上昇し
たときに処理槽Ｂへの送液と処理槽Ｂの曝気、処
理槽Ａへの返送を停止し、処理槽Ｂの活性汚泥を
分離し、その分離水及び分離汚泥の一部を系外へ
排出したのち、前記処理槽Ｂへの送液、曝気、処
理槽Ａへの返送を再開するサイクルを繰返すこと
を特徴とする排水の生物学的処理方法である。
In the present invention, when treating wastewater using a treatment tank A in which wastewater continuously flows in, the water level fluctuates up and down, and is in an anaerobic atmosphere, and a treatment tank B in an aerobic condition, the treatment tank A The liquid is sent to treatment tank B for aeration, and the liquid that is sent is returned from treatment tank B to treatment tank A. When the water level in treatment tank A rises to a predetermined water level, the liquid is sent to treatment tank B. After stopping liquid feeding, aeration of treatment tank B, and return to treatment tank A, separating activated sludge in treatment tank B, and discharging a portion of the separated water and separated sludge to the outside of the system, the treatment tank B This is a biological treatment method for wastewater, which is characterized by repeating the cycle of sending liquid to the tank A, aeration, and restarting the return to the treatment tank A.
本発明の一例を図面を参照しながら説明する
と、第１図示例において、原排水１は処理槽Ａへ
連続して流入し、後述する返送された活性汚泥が
浮遊する返送液５と混合される。処理槽Ａは、好
ましくは溶存酸素が０〜1.0mg／程度に維持さ
れた嫌気的雰囲気になつており、前記返送液５中
に含有されているNOx（NO2，NO3など）は、原
排水１中に含有されているBOD物質によつて生
物学的にN2ガスに還元、脱窒され、液中から放
散される。このように処理槽Ａにて処理された混
合液は、次いでポンプ２によつて処理槽Ｂに送液
され、ブロワ３から散気装置４を経て吹込まれる
空気によつて曝気され、好気的条件下で液中に残
留するBOD物質が酸化分解され、アンモニア等
の窒素は硝化されてNOxが生成される。この場
合、処理槽Ａでは嫌気的雰囲気において返送液５
中の活性汚泥からリンが溶出するが、処理槽Ｂの
好気的条件下では逆にリンが活性汚泥に吸収され
る。この吸収されるリンの量は、処理槽Ａで溶出
した量よりも多く、このため原排水１中のリンの
一部あるいは大部は処理槽Ｂで液中から除去さ
れ、活性汚泥中に蓄積される。また、BOD物質
を処理槽Ａの嫌気的雰囲気で吸着させることによ
り、活性汚泥中に非バルキング性の微生物が優占
種となり、汚泥の圧密性、沈降性が大幅に改良さ
れる。
An example of the present invention will be described with reference to the drawings. In the first illustrated example, raw wastewater 1 continuously flows into a treatment tank A, and is mixed with a return liquid 5 in which returned activated sludge, which will be described later, is suspended. . The treatment tank A preferably has an anaerobic atmosphere in which dissolved oxygen is maintained at about 0 to 1.0 mg/distance, and the NOx (NO 2 , NO 3 , etc.) contained in the returned liquid 5 is The BOD substance contained in the wastewater 1 biologically reduces it to N2 gas, denitrifies it, and releases it from the liquid. The mixed liquid treated in the treatment tank A is then sent to the treatment tank B by the pump 2, and is aerated with air blown from the blower 3 through the aeration device 4. Under normal conditions, BOD substances remaining in the liquid are oxidized and decomposed, nitrogen such as ammonia is nitrified, and NOx is generated. In this case, in the treatment tank A, the return liquid 5 is
Phosphorus is eluted from the activated sludge inside, but under the aerobic conditions of treatment tank B, phosphorus is absorbed into the activated sludge. The amount of phosphorus absorbed is greater than the amount eluted in treatment tank A, so some or most of the phosphorus in raw wastewater 1 is removed from the solution in treatment tank B and accumulated in the activated sludge. be done. Furthermore, by adsorbing BOD substances in the anaerobic atmosphere of treatment tank A, non-bulking microorganisms become the dominant species in the activated sludge, and the compaction and settling properties of the sludge are greatly improved.
処理槽Ｂに送液された処理槽Ａの混合液は曝気
処理されたのち、処理槽Ａからの送液分を返送液
５として処理槽Ａへ返送し、再び嫌気的雰囲気下
において原排水１とともに処理される。返送液５
は、処理槽Ａと処理槽Ｂが隔離配置されていると
きは、ポンプ輸送などで返送することもできる
が、図示例のように両槽Ａ，Ｂを隣接せしめ、処
理槽Ｂの水位を処理槽Ａより高く維持し、溢流壁
６から直接溢流させて返送できるようにするのが
便利である。 The mixed liquid in treatment tank A sent to treatment tank B is aerated, and then the liquid sent from treatment tank A is sent back to treatment tank A as return liquid 5, and the raw wastewater 1 is returned to treatment tank A under an anaerobic atmosphere. Processed with Return liquid 5
When treatment tank A and treatment tank B are placed in isolation, the water can be returned by pump transportation, but as shown in the example, it is possible to place both tanks A and B next to each other and treat the water level in treatment tank B. It is convenient to maintain it higher than tank A so that it can be directly overflowed from overflow wall 6 and returned.
このように、混合液が嫌気、好気条件下を繰り
返し経由することによつて、窒素の除去及び活性
汚泥のリン蓄積機能、非バルキング化に寄与す
る。しかるに、一過性の処理及び両槽Ａ，Ｂが共
に嫌気的雰囲気、あるいは好気的条件では、この
ような処理機能は発現しない。 In this way, by repeatedly passing the mixed liquid through anaerobic and aerobic conditions, it contributes to nitrogen removal, phosphorus accumulation function of activated sludge, and non-bulking. However, such a processing function does not occur when the treatment is temporary or when both tanks A and B are in an anaerobic atmosphere or under aerobic conditions.
前述のように、処理槽Ａから処理槽Ｂに送液さ
れた液は、曝気を受けて酸化され、再び処理槽Ａ
に返送されるが、以下これらを曝気工程と呼べ
ば、原排水１の連続流入によつて処理槽Ａ内の水
位が上昇して水位検出部７に達すると、あるいは
あらかじめタイマにて設定された時間が経過する
と、曝気工程が終了する。すなわち、液の処理槽
Ｂへの送液、曝気、処理槽Ａへの返送を停止し、
処理槽Ｂ中の浮遊汚泥を分離し、分離水８は処理
水として排出され、分離汚泥の一部は余剰汚泥９
としてポンプ１０などにて引き抜かれる。 As mentioned above, the liquid sent from treatment tank A to treatment tank B is aerated and oxidized, and then transferred to treatment tank A again.
Hereinafter, these steps will be referred to as the aeration process.When the water level in the treatment tank A rises due to the continuous inflow of the raw wastewater 1 and reaches the water level detection part 7, or when the water level is set in advance by a timer. Once the time has elapsed, the aeration process ends. That is, stopping the liquid feeding to the processing tank B, aeration, and returning the liquid to the processing tank A,
Floating sludge in treatment tank B is separated, separated water 8 is discharged as treated water, and a part of the separated sludge is used as surplus sludge 9.
It is pulled out by a pump 10 or the like.
また、前記曝気工程以外の時間帯を分離工程と
呼べば、分離工程で汚泥の分離、分離水８の排
出、余剰汚泥９の引抜きが行われるが、分離水８
の排出と余剰汚泥９の引抜きは同時に行うことも
可能である。またこの分離工程中にも原排水は処
理槽Ａ内に流入している。 In addition, if the time period other than the aeration process is called a separation process, in the separation process, separation of sludge, discharge of separated water 8, and extraction of excess sludge 9 are performed.
It is also possible to discharge the sludge 9 and extract the excess sludge 9 at the same time. Also, raw wastewater is flowing into the treatment tank A during this separation process.
分離工程では、各操作時間をタイマにて設定制
御するとよい。例えば第２図に示すように、汚泥
の分離をタイマ制御T1、分離水８の排出をタイ
マ制御T2、余剰汚泥９の引抜きをタイマ制御T3
として制定するが、処理槽Ｂに汚泥濃度検出器
（図示せず）を配備して、汚泥界面が所定の位置
より低下してから分離水８の排出、余剰汚泥９の
引抜きを行うことも可能である。その場合、汚泥
濃度検出器の汚れによる誤動作を防止するため、
汚泥濃度検出器は自動あるいは手動で必要に応じ
て洗浄しなければならない。 In the separation process, it is preferable to set and control each operation time using a timer. For example, as shown in FIG. 2, the separation of sludge is controlled by a timer T 1 , the discharge of separated water 8 is controlled by a timer T 2 , and the extraction of excess sludge 9 is controlled by a timer T 3
However, it is also possible to install a sludge concentration detector (not shown) in the treatment tank B and discharge the separated water 8 and pull out the excess sludge 9 after the sludge interface has fallen below a predetermined level. It is. In that case, to prevent malfunction due to dirt on the sludge concentration detector,
Sludge concentration detectors must be cleaned automatically or manually as necessary.
分離工程が終了したのちは再び曝気工程が再開
され、第２図に示すように制御される。すなわ
ち、分離工程中にも処理槽Ａには原排水１が流入
し、その水位は水位検出部７よりも高くなる。曝
気工程はタイマ制御T4で所定時間行われるが、
曝気工程開始と同時に処理槽Ｂに送液されるた
め、分離排出した分離水８と引き抜かれた余剰汚
泥９の分だけ処理槽Ａの水位WL1が低下し、水
位により制御された曝気工程Ｌが行われ、次に水
位が水位検出部７に到達するWL2まで続けられ
る。水位制御Ｌによる曝気工程は、原排水１の量
の変動によつて変り、水量が多いと短かくなり、
反対に水量が少なくなると長くなるが、曝気時間
は原排水１の汚濁成分濃度、槽内の汚泥濃度によ
つて変つてくるから、これらの条件を考慮して必
要とする曝気時間に対応して槽の容積、面積を決
めるとよい。 After the separation process is completed, the aeration process is restarted and controlled as shown in FIG. That is, the raw wastewater 1 flows into the treatment tank A even during the separation process, and its water level becomes higher than the water level detection part 7. The aeration process is carried out for a predetermined time using timer control T4 .
Since the liquid is sent to the treatment tank B at the same time as the start of the aeration process, the water level WL 1 of the treatment tank A is lowered by the amount of the separated water 8 that has been separated and discharged and the excess sludge 9 that has been pulled out, and the aeration process L is controlled by the water level. is carried out, and then continues until WL 2 when the water level reaches the water level detection section 7. The aeration process using water level control L changes depending on the amount of raw wastewater 1, and becomes shorter when the amount of water is large.
On the other hand, when the amount of water decreases, the aeration time becomes longer, but since the aeration time varies depending on the concentration of pollutant components in the raw wastewater 1 and the concentration of sludge in the tank, take these conditions into account and adjust the aeration time required. It is a good idea to determine the volume and area of the tank.
また、分離工程中、原排水が処理槽Ａに大量に
流入し、タイマ制御T4による曝気工程開始後所
定時間を経過しても水位WL1が水位検出部７以
下に低下しないときは、曝気工程はタイマ制御
T5により延長継続するようにするとよい。この
タイマ制御T5による時間は処理槽Ａの水位が下
がるように、水位制御Ｌによる曝気工程より短か
く設定する。例えば、水位及びタイマによつて１
サイクル６時間（曝気工程５時間、分離工程１時
間）の設定で、水位WL1が水位検出部７以下に
低下しない場合は、第３図のタイムダイアグラム
に示すようにタイマ制御T5による曝気工程を３
時間程度に設定しておき、これによつて水位が１
サイクル後に水位検出部７以下に下がつたら、再
び水位制御Ｌによる曝気工程が設定されるように
自動制御するとよい。 In addition, during the separation process, if a large amount of raw wastewater flows into the treatment tank A and the water level WL 1 does not fall below the water level detection part 7 even after a predetermined time has elapsed after the start of the aeration process by timer control T 4 , the aeration Process is timer controlled
It is recommended to continue extending with T 5 . The time set by the timer control T5 is set to be shorter than the aeration process set by the water level control L so that the water level of the treatment tank A is lowered. For example, 1 depending on the water level and timer.
If the water level WL 1 does not fall below water level detection part 7 when the cycle is set to 6 hours (aeration process 5 hours, separation process 1 hour), the aeration process is started by timer control T 5 as shown in the time diagram in Figure 3. 3
Set the water level to about 1 hour.
It is preferable to perform automatic control so that when the water level drops below the water level detection part 7 after the cycle, the aeration process by the water level control L is set again.
なお、本発明では、分離工程においても分離水
８と原排水１を完全に隔離して、原排水１を連続
的に投入可能となつているから、第１図示例の水
位検出部７の位置を、分離工程中に処理槽Ａの水
位が溢流壁６の高さ以上にならないように設定す
る。 In addition, in the present invention, even in the separation process, the separated water 8 and the raw waste water 1 are completely separated and the raw waste water 1 can be continuously introduced, so the position of the water level detection part 7 in the first illustrated example is is set so that the water level in the treatment tank A does not exceed the height of the overflow wall 6 during the separation process.
処理槽Ａにおける撹拌は、回転式撹拌機等の機
械式撹拌、あるいは少量の空気を用いて行つても
よいが、原排水１や返送液５の流下エネルギだけ
でも可能である。原排水１や返送液５の流下エネ
ルギだけで処理槽Ａ内を混合する場合には、槽の
面積、水深に対して流入水量、流入高さと水位と
の差を大きくとればよい。しかしながら、流下時
の水面の乱れによつて液中に多量の酸素が気相か
ら移動し、好気的条件となつて処理槽Ａにおける
脱窒、脱リン作用を阻害する場合には、逆に水位
差を小さくするか、あるいは第４図示例の如く、
原排水１の流入口を水面下にし、処理槽Ｂからの
返送液５の溢流部に整流板１１あるいは溢流管を
設けるとよい。 Stirring in the treatment tank A may be performed by mechanical stirring such as a rotary stirrer or by using a small amount of air, but it is also possible to use only the flowing energy of the raw wastewater 1 or the returned liquid 5. When mixing the inside of the treatment tank A using only the flowing energy of the raw wastewater 1 and the returned liquid 5, it is sufficient to make a large difference between the amount of inflow water, the height of the inflow, and the water level with respect to the area and water depth of the tank. However, if a large amount of oxygen moves from the gas phase into the liquid due to turbulence on the water surface during flowing down, creating an aerobic condition that inhibits the denitrification and dephosphorization effects in treatment tank A, the opposite occurs. Either reduce the water level difference, or as shown in the fourth example,
It is preferable that the inlet of the raw wastewater 1 is placed below the water surface, and a rectifier plate 11 or an overflow pipe is provided at the overflow part of the return liquid 5 from the treatment tank B.
原排水１の窒素除去率は返送液５の量で決ま
り、返送量が多いほど処理槽Ｂで生成したNOx
が処理槽Ａに返流して除去される。例えば返送液
量が原排水１の流入量と等量であれば、除去率は
50％となる。返送液量は希望する除去率に応じて
設定するとよいが、過剰な返送、例えば原排水１
に対して50〜100倍の循環はポンプ稼動時の電力
消費量を増加し、また処理槽Ｂから処理槽Ａへの
溶存酸素持ち込み量が多くなつて、処理槽Ａの嫌
気的雰囲気が損われるので好ましくない。 The nitrogen removal rate of raw wastewater 1 is determined by the amount of returned liquid 5, and the larger the returned amount, the more NOx generated in treatment tank B.
is returned to treatment tank A and removed. For example, if the amount of returned liquid is equal to the amount of inflow of raw wastewater 1, the removal rate is
It will be 50%. The amount of returned liquid should be set according to the desired removal rate, but if excessive return is required, for example raw wastewater 1
Circulating 50 to 100 times the amount of water increases power consumption during pump operation, and also increases the amount of dissolved oxygen carried from treatment tank B to treatment tank A, impairing the anaerobic atmosphere in treatment tank A. So I don't like it.
また、本発明では、BODの存在しない排水で
は、窒素、リンの除去ができないので、その場合
にはBOD含有排水と混合処理するか、あるいは
新たにBOD源を添加するとよい。 Furthermore, in the present invention, nitrogen and phosphorus cannot be removed from wastewater that does not contain BOD, so in that case, it is preferable to mix the wastewater with BOD-containing wastewater or add a new BOD source.
なお、第１図及び第４図示例では、処理槽Ａの
混合液をポンプ２によつて処理槽Ｂに送液してい
るが、通常のポンプのほかエアリフトポンプを用
いると送液と共に酸素の補給も行うことができ
る。また、分離水８の排出は弁、ゲート等を用い
て自然流下で排出するとよく、余剰汚泥の引抜き
は、ポンプのほか弁を用いて水圧により自動的に
排出するようにしてもよい。処理槽Ｂを好気的条
件下に保持するための曝気は、酸素を供給する方
法ならば如何なる方法も利用可能であるが、散気
方式を用いる場合は、散気停止時の逆圧で散気部
の目詰まりが生じないような散気装置を配備する
とよい。 In the examples shown in FIGS. 1 and 4, the mixed liquid in the treatment tank A is sent to the treatment tank B by the pump 2, but if an air lift pump is used in addition to a normal pump, oxygen will be pumped together with the liquid. Replenishment can also be done. Further, the separated water 8 may be discharged by gravity using a valve, a gate, etc., and the excess sludge may be automatically discharged by water pressure using a valve in addition to a pump. Any method can be used for aeration to maintain treatment tank B under aerobic conditions as long as it supplies oxygen, but when using the aeration method, it is possible to aerate using the back pressure when the aeration is stopped. It is advisable to provide an air diffuser that will prevent clogging of air areas.
さらに本発明の一実施例を示せば、次の通りで
ある。
Further, an embodiment of the present invention is as follows.
BOD200mg／、NH3―N20mg／、PO3- 410
mg／の生活系排水を用い、処理槽Ｂで１時間浮
遊活性汚泥を沈降分離したのち、20分間で分離水
と余剰汚泥の排出を行つたあと、６時間液の循
環、曝気するサイクルで嫌気的雰囲気にある処理
槽Ａの水位検出部に水位が到達するように水量負
荷を設定した結果、槽内のMLSS6200mg／、平
均BOD7mg／、NH3―N0.5mg／、NOx―
N2.7mg／、PO3- 41.7mg／（PO3- 4の除去率は
BOD、NH3―Ｎに比べて若干不安定であり、変
動幅としては処理水PO3- 40.8〜3.1mg／であつ
た）の処理水が得られ、また活性汚泥の沈降性も
SVI30分53％（MLSS6200mg／）ときわめて良
好な処理を行うことができた。この場合の循環液
量は流入排水量の５倍に設定した。 BOD200mg/, NH 3 -N20mg/, PO 3- 4 10
mg/mg of domestic wastewater, the floating activated sludge is sedimented and separated in treatment tank B for 1 hour, the separated water and excess sludge are discharged for 20 minutes, and then the liquid is circulated and aerated for 6 hours in an anaerobic cycle. As a result of setting the water load so that the water level reaches the water level detection part of treatment tank A in a normal atmosphere, the MLSS in the tank is 6200mg/, the average BOD is 7mg/, NH 3 -N0.5mg/, NOx-
N2.7mg/, PO 3-4 1.7mg/(The removal rate of PO 3-4 is
BOD, NH 3 - It is slightly unstable compared to N, and the range of fluctuation was 0.8 to 3.1 mg of treated water PO 3- 4 ) was obtained, and the settling property of activated sludge was also
Very good treatment was achieved with an SVI of 53% (MLSS of 6200mg/) in 30 minutes. The amount of circulating fluid in this case was set to five times the amount of inflow drainage.
また、循環、曝気時間をタイマで５時間に設定
したが、ほぼ同等の水質を得ることができた。さ
らに処理槽Ｂの汚泥沈降界面を光電方式の界面計
で検知してから分離水の排出を行つたところ、沈
降分離時間を40分に短縮することができた。 Although the circulation and aeration time was set to 5 hours using a timer, almost the same water quality could be obtained. Furthermore, by detecting the sludge settling interface in treatment tank B with a photoelectric interface meter before discharging the separated water, the settling time was able to be shortened to 40 minutes.
なお、本実施例は自動制御で行つたものであ
り、無人で難なく生活系排水の処理を行うことが
でき、処理槽Ａの溶存酸素は０〜1.0mg／で変
動し、処理槽Ｂの溶存酸素は1.5mg／以上であ
つた。 In addition, this example was carried out using automatic control, and domestic wastewater can be treated unattended and without difficulty.Dissolved oxygen in treatment tank A fluctuates from 0 to 1.0 mg/ Oxygen was more than 1.5mg/.
以上述べたように本発明によれば、次のような
きわめて有益なる効果を奏することができる。
As described above, according to the present invention, the following extremely beneficial effects can be achieved.
簡単な装置で操作容易に、排水中のBOD、
窒素、リンなどを効率よく除去することができ
る。 Easy to operate with simple equipment, BOD in drainage,
Nitrogen, phosphorus, etc. can be removed efficiently.
連続的に処理をしても、処理水が混合するこ
とが全くないから、従来の貯留槽が不要にな
り、かつ高度に処理された処理水を得ることが
できる。 Even if the treatment is carried out continuously, the treated water does not mix at all, so a conventional storage tank is not required, and highly treated treated water can be obtained.
活性汚泥の沈降性、濃縮性が大幅に改善され
ることによつて、汚泥の分離が容易になり、清
澄な処理水と高濃度の余剰汚泥を得ることがで
きる。 By significantly improving the sedimentation and thickening properties of activated sludge, the sludge can be easily separated, and clear treated water and highly concentrated surplus sludge can be obtained.
図面は本発明の実施態様を示すもので、第１図
は系統説明図、第２図は本発明の制御方法を示す
説明図、第３図は第２図に基く設定例のタイムダ
イアグラムを示し、第４図はさらに他の例を示す
系統説明図である。
１…原排水、２，１０…ポンプ、３…ブロワ、
４…散気装置、５…返送液、６…溢流壁、７…水
位検出部、８…分離水、９…余剰汚泥、１１…整
流板。
The drawings show embodiments of the present invention; FIG. 1 is an explanatory diagram of the system, FIG. 2 is an explanatory diagram showing the control method of the present invention, and FIG. 3 is a time diagram of a setting example based on FIG. 2. , FIG. 4 is a system explanatory diagram showing still another example. 1... Raw wastewater, 2, 10... Pump, 3... Blower,
4... Aeration device, 5... Return liquid, 6... Overflow wall, 7... Water level detection section, 8... Separated water, 9... Excess sludge, 11... Rectifier plate.
Claims (1)
嫌気的雰囲気にある処理槽Ａと、好気的条件下に
ある処理槽Ｂを用いて排水を処理するに際し、処
理槽Ａの液を処理槽Ｂに送液して曝気するととも
にこの送液分の液を処理槽Ｂから処理槽Ａへ返送
し、処理槽Ａの水位が所定水位に上昇したときに
処理槽Ｂへの送液と処理槽Ｂの曝気、処理槽Ａへ
の返送を停止し、処理槽Ｂの活性汚泥を分離し、
その分離水及び分離汚泥の一部を系外へ排出した
のち、前記処理槽Ｂへの送液、曝気、処理槽Ａへ
の返送を再開するサイクルを繰返すことを特徴と
する排水の生物学的処理方法。 ２ 前記処理槽Ａと処理槽Ｂを隣接せしめ、処理
槽Ｂの水位を処理槽Ａより高く維持し、かつ処理
槽Ｂから処理槽Ａへ溢流可能に配列したものであ
る特許請求の範囲第１項記載の排水の生物学的処
理方法。 ３ 前記サイクルをタイマ及び処理槽Ａの水位設
定により制御するものである特許請求の範囲第１
項又は第２項記載の排水の生物学的処理方法。 ４ 前記処理槽Ｂにおける分離水及び分離汚泥の
系外への排出が該槽の汚泥界面を検知して行われ
るものである特許請求の範囲第１項〜第３項のい
ずれか一つの項記載の排水の生物学的処理方法。 ５ 前記処理槽Ａの溶存酸素を０〜1.0mg／に
維持するものである特許請求の範囲第１項〜第４
項のいずれか一つの項記載の排水の生物学的処理
方法。[Scope of Claims] 1. When treating wastewater using a treatment tank A in which wastewater continuously flows in, the water level moves up and down, and is in an anaerobic atmosphere, and a treatment tank B is in an aerobic condition, The liquid in treatment tank A is sent to treatment tank B for aeration, and the liquid equivalent to this sent liquid is returned from treatment tank B to treatment tank A. When the water level in treatment tank A rises to a predetermined water level, the treatment tank Stop sending liquid to B, aerating treatment tank B, and returning to treatment tank A, and separate activated sludge from treatment tank B.
Biological treatment of wastewater characterized by repeating a cycle of discharging a part of the separated water and separated sludge outside the system, and then restarting the cycle of sending liquid to the treatment tank B, aeration, and returning to the treatment tank A. Processing method. 2. The treatment tank A and the treatment tank B are arranged adjacent to each other, the water level of the treatment tank B is maintained higher than that of the treatment tank A, and the water level of the treatment tank B is maintained so as to overflow from the treatment tank B to the treatment tank A. The biological treatment method for wastewater according to item 1. 3. Claim 1, wherein the cycle is controlled by a timer and water level setting of treatment tank A.
The method for biological treatment of wastewater according to paragraph 2 or paragraph 2. 4. Any one of claims 1 to 3, wherein the separated water and separated sludge in the treatment tank B are discharged to the outside of the system by detecting the sludge interface of the tank. biological treatment method for wastewater. 5 Claims 1 to 4 which maintain the dissolved oxygen in the treatment tank A at 0 to 1.0 mg/
A biological treatment method for wastewater as described in any one of the following paragraphs.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10952484A JPS60255198A (en) | 1984-05-31 | 1984-05-31 | Biological treatment of waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP10952484A JPS60255198A (en) | 1984-05-31 | 1984-05-31 | Biological treatment of waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS60255198A JPS60255198A (en) | 1985-12-16 |
| JPS6366597B2 true JPS6366597B2 (en) | 1988-12-21 |
Family
ID=14512436
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP10952484A Granted JPS60255198A (en) | 1984-05-31 | 1984-05-31 | Biological treatment of waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS60255198A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS63158197A (en) * | 1986-12-22 | 1988-07-01 | Ebara Infilco Co Ltd | Treatment of ammonia-containing waste water |
| JPH0732911B2 (en) * | 1989-11-21 | 1995-04-12 | 荏原インフイルコ株式会社 | How to recycle filter media |
| CZ2022380A3 (en) * | 2022-09-07 | 2023-11-29 | Jan Topol | Waste water treatment method and equipment for carrying out the method |
-
1984
- 1984-05-31 JP JP10952484A patent/JPS60255198A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS60255198A (en) | 1985-12-16 |
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