JPS63104699A - Method for controlling operation of anaerobic tank by underwater stirrer - Google Patents
Method for controlling operation of anaerobic tank by underwater stirrerInfo
- Publication number
- JPS63104699A JPS63104699A JP24895686A JP24895686A JPS63104699A JP S63104699 A JPS63104699 A JP S63104699A JP 24895686 A JP24895686 A JP 24895686A JP 24895686 A JP24895686 A JP 24895686A JP S63104699 A JPS63104699 A JP S63104699A
- Authority
- JP
- Japan
- Prior art keywords
- anaerobic
- aerobic
- activated sludge
- tanks
- tank
- 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 34
- 239000010802 sludge Substances 0.000 claims abstract description 38
- 238000011282 treatment Methods 0.000 claims abstract description 24
- 238000006243 chemical reaction Methods 0.000 claims description 16
- 238000003756 stirring Methods 0.000 abstract description 39
- 230000008859 change Effects 0.000 abstract description 3
- 238000013019 agitation Methods 0.000 description 21
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 11
- 229910052760 oxygen Inorganic materials 0.000 description 11
- OAICVXFJPJFONN-UHFFFAOYSA-N Phosphorus Chemical compound [P] OAICVXFJPJFONN-UHFFFAOYSA-N 0.000 description 9
- 229910052698 phosphorus Inorganic materials 0.000 description 9
- 239000011574 phosphorus Substances 0.000 description 9
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 239000002351 wastewater Substances 0.000 description 6
- 239000007788 liquid Substances 0.000 description 5
- 229910052757 nitrogen Inorganic materials 0.000 description 5
- 230000000694 effects Effects 0.000 description 4
- 238000004062 sedimentation Methods 0.000 description 4
- 239000010865 sewage Substances 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 230000005587 bubbling Effects 0.000 description 2
- 238000011835 investigation Methods 0.000 description 2
- 238000005086 pumping Methods 0.000 description 2
- 239000011435 rock Substances 0.000 description 2
- 238000011144 upstream manufacturing Methods 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 230000002411 adverse Effects 0.000 description 1
- 230000008901 benefit Effects 0.000 description 1
- 239000003638 chemical reducing agent Substances 0.000 description 1
- 238000004891 communication Methods 0.000 description 1
- 230000008094 contradictory effect Effects 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000001514 detection method Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 238000004134 energy conservation Methods 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 238000009775 high-speed stirring Methods 0.000 description 1
- 239000010800 human waste Substances 0.000 description 1
- 230000006872 improvement Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 238000010907 mechanical stirring Methods 0.000 description 1
- 230000002503 metabolic effect Effects 0.000 description 1
- 239000010813 municipal solid waste Substances 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 235000015097 nutrients Nutrition 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 230000008569 process Effects 0.000 description 1
- 238000012545 processing Methods 0.000 description 1
- 230000009467 reduction Effects 0.000 description 1
- 238000011160 research Methods 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 238000007790 scraping Methods 0.000 description 1
- 230000001932 seasonal effect Effects 0.000 description 1
- 238000012546 transfer Methods 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【発明の詳細な説明】
〈産業上の利用分野〉
本発明は、下水・し尿・ごみ汁廃水・工場廃水などの各
分野における汚水を対象とした水中攪拌機による嫌気槽
の運転制御方法に関する。DETAILED DESCRIPTION OF THE INVENTION <Field of Industrial Application> The present invention relates to a method for controlling the operation of an anaerobic tank using a submersible agitator for wastewater in various fields such as sewage, human waste, garbage water wastewater, and factory wastewater.
く従来技術〉
有機廃水浄化処理の方法として従来広く用いられてきた
通常の活性汚泥法は、窒素、燐等栄養塩類の満足な除去
が得られず、このため内海あるいは湖沼等、閉鎖性水域
の富栄養化による各種弊害を招いていることは一般に知
られているとおりで、これを防止までは改善するため、
下水・舅尿をはじめ各種汚水から窒素・燐を除去するこ
とが社会的課題となっており、これまで各種方法、ｖｔ
置例えば特許第９３６２９３号並びに特許第１１４７２
６９号案が開発検討されてきたが、長斯間に亘り国内に
広く普及した活性汚泥法とその施設の効用を図る観、α
より、その目的を達するに当たっては嫌気・好気活性汚
泥法が注目されるに至っている。Conventional technology> The conventional activated sludge method, which has been widely used as a method for purifying organic wastewater, cannot satisfactorily remove nutrient salts such as nitrogen and phosphorus. It is generally known that eutrophication causes various adverse effects, and in order to prevent or improve this,
Removing nitrogen and phosphorus from various types of wastewater, including sewage and father's urine, has become a social issue.
For example, Patent No. 936293 and Patent No. 11472
Plan No. 69 has been under consideration for development, but the activated sludge method, which has been widely used throughout the country during the Nagasaki period, and the concept of improving the effectiveness of its facilities, α
Therefore, anaerobic/aerobic activated sludge methods are attracting attention in achieving this goal.
嫌気・好気活性汚泥法による窒素、燐除去の方法の内先
ず窒素除去については、好気槽（以下、○糟と謂う）に
於いて活性汚泥の生物反応により硝酸化、亜硝酸化した
窒素成分を無酸素の嫌気槽（以下、Ａ梢と謂う）で脱窒
し、窒素ガスとして大気中に発散させる。Among the methods for removing nitrogen and phosphorus using the anaerobic/aerobic activated sludge method, the first step is to remove nitrogen through nitrification and nitrite oxidation through biological reactions in activated sludge in an aerobic tank (hereinafter referred to as ○kasu). The components are denitrified in an oxygen-free anaerobic tank (hereinafter referred to as A-tree) and released into the atmosphere as nitrogen gas.
燐については同じく活性汚泥の燐に対する生物反応によ
る。即ち、有機物存在下のＡ槽で体内の燐を放出した活
性汚泥は、次の○槽で前記放出量以上の燐を体内に摂取
するという活性汚泥の燐代謝特性を利用する。Regarding phosphorus, it is also due to the biological reaction to phosphorus in activated sludge. That is, activated sludge that releases phosphorus from the body in tank A in the presence of organic matter takes advantage of the phosphorus metabolic characteristics of activated sludge, such that in the next tank ○, more phosphorus than the released amount is taken into the body.
この原理に基づく嫌気・好気活性汚泥法には、硝化液循
環法、非循環法、Ｂ ｕｒｄｅｎｐｈｏ法などがあり、
対象とする汚水の成分や目標処理水質等、処理条件に応
じた選択がおこなわれている。Anaerobic/aerobic activated sludge methods based on this principle include the nitrification liquid circulation method, non-circulation method, and Burdenpho method.
Selection is made according to treatment conditions, such as target wastewater components and target treated water quality.
何れの処理方法に於いてもＡＷｉとＯ槽がもうけられる
が、この相反する槽内環境の両者に共通する必要機能は
攪拌である。In either treatment method, an AWi tank and an O tank are created, but the necessary function common to both of these contradictory tank environments is stirring.
攪拌の手段は通常、機械攪拌と空気攪拌が考えられ、空
気攪拌とした場合は混合液中に酸素の移動が起こるので
、好気攪拌が行える反面、嫌気ゾーンが実現せず、よっ
てＡ槽には従来よＱｔｆｉ械攪拌方式が多く採用されて
きたが、０槽に散気板、故気筒等単−機能が採用されて
いる限りに於いては、当初上りＡ槽と０槽の容量比なら
びに配置が固定されているに等しい。Mechanical agitation and air agitation are usually considered as the means of agitation.If air agitation is used, oxygen will move into the mixed liquid, allowing aerobic agitation, but on the other hand, an anaerobic zone will not be created, and therefore Conventionally, the Qtfi mechanical stirring system has been widely adopted, but as long as single functions such as a diffuser plate and a dead cylinder are used in the 0 tank, the initial capacity ratio between the upstream A tank and the 0 tank, It is equivalent to having a fixed position.
生物反応を原理とする活性汚泥法は温度の影響が大であ
る。The activated sludge method, which is based on biological reactions, is greatly affected by temperature.
生物反応速度は温度に密接に関係し、脱窒速度、硝化速
度の比も温度によって変わってくる。このような場合Ａ
槽と○槽の容量比を変更すれば合理的な処理を行うこと
ができるが、上記のように機能的に容量比が固定されて
いるに等しい従来技術ではこれが不可能であった。Biological reaction rates are closely related to temperature, and the ratio of denitrification rate to nitrification rate also changes depending on temperature. In such a case A
Although it is possible to carry out rational processing by changing the capacity ratio between the tank and the ○ tank, this was not possible with the conventional technology in which the capacity ratio is functionally fixed as described above.
またＡｆｆｉに於いては活性汚泥が沈澱しない最低限度
の攪拌強度で処理を行うことがエネルギー消費の観点で
は最も合理的であるが、活性汚泥の沈澱しない最低限度
は、流入水質や処理条件によって生成される活性汚泥の
性状によって異なってくる。そのため、従来は安全を見
込んで必要以上の攪拌を行い、エネルギーを無駄に消費
する傾向があった。Furthermore, in terms of energy consumption, it is most rational to perform treatment at the minimum agitation intensity that does not cause activated sludge to settle in Affi, but the minimum amount of agitation that does not allow activated sludge to settle depends on the quality of the influent water and the treatment conditions. It varies depending on the properties of activated sludge. Therefore, in the past, there has been a tendency to perform more stirring than necessary in consideration of safety, which wastes energy.
〈発明が解決しようとする問題点〉
流入汚水の温度、水量、水質等、季節変動に対して適切
な生物反応環境を一定′８′積の中でつくり出すことに
より、従来技術が達し得ながった下記問題点を解決する
。<Problem to be solved by the invention> By creating a biological reaction environment within a constant volume that is suitable for seasonal changes in temperature, water volume, water quality, etc. of inflowing sewage, it is possible to solve problems that the conventional technology could not achieve. The following problems were solved.
■Ａ［とＯ槽の容量比ならびに配置を自由に変更し得る
装置の実現。■Realization of a device in which the capacity ratio and arrangement of A and O tanks can be freely changed.
■Ａ槽に於いて、生物反応速度を低下させない必要最少
攪拌強度の探知と、その維持。■Detection and maintenance of the minimum required stirring intensity that does not reduce the rate of biological reaction in tank A.
〈問題点を解決するための手段〉
嫌気・好気活性汚泥法に於いて、仕切られた複数個の生
物反応槽の夫々の区分に嫌気・好気両用水中攪拌様を設
置して、嫌気槽或は好気槽の何れにも変換できるように
すると共に、該嫌気槽と好気槽の容量比と配置何れをも
自由に変更１．得るようにして嫌気・好気活性汚泥処理
を可能にし、前記全攪拌への内任意台数の攪拌強度を、
処ｐ！、目的に照らし、嫌気槽を活性汚泥濃度に応じて
、自動連続的に、或は自動間歇的に、或は適宜手動操作
で制御する。<Means for solving the problem> In the anaerobic/aerobic activated sludge method, an anaerobic/aerobic underwater stirring system is installed in each section of multiple partitioned biological reaction tanks, and the anaerobic tank is Alternatively, it can be converted to either an aerobic tank, and the capacity ratio and arrangement of the anaerobic tank and aerobic tank can be freely changed.1. It enables anaerobic/aerobic activated sludge treatment in such a way that the agitation intensity of an arbitrary number of units is added to the total agitation.
Where p! Depending on the purpose, the anaerobic tank is automatically controlled continuously, automatically intermittently, or manually as appropriate depending on the activated sludge concentration.
ぐ実施例〉 以下、本発明について実施例により現明する。Examples Hereinafter, the present invention will be elucidated by way of examples.
第１図に示すように、一定容積の生物反応槽１を隔Ｉ！
！２ 、２・・・で仕切って連続セル３．３・・・とな
し、各セル３，３・・・に第２図（ａ）または１図（ｂ
）に示すように、上記、嫌気・好気両用水中攪拌様４を
設置し、全磯に空気配Ｉｒ７Ｇを施してブロワ−５がら
送気可能ならしめれば、ＡｍとＯ槽の容量比ならびに配
置を自由に変更することができる。尚、ｆｊｒＪ２図（
ｂ）は深底槽反応槽の例を示す。As shown in FIG. 1, a biological reaction tank 1 with a constant volume is separated by I!
! 2, 2... are divided into consecutive cells 3, 3..., and each cell 3, 3... is divided by Figure 2 (a) or Figure 1 (b).
), if the above-mentioned anaerobic/aerobic underwater agitation type 4 is installed and the air distribution Ir7G is applied to the entire rocky shore so that air can be supplied from the blower 5, the capacity ratio of the Am and O tanks and the The arrangement can be changed freely. In addition, fjrJ2 figure (
b) shows an example of a deep-bottom reactor.
例えば、Ａ梢と０４１１ＩＩの配置Ｖ＃戊によって第３
図（ａ）、第３図（ｂ）のような硝化液循環法、又は第
３図（ｃ）、第３図（ｄ）のような非循環法、第３図（
ｅ）、第３図（ｆ）のようなりａｒｄｅｎｐｈｏ法など
が自由に選択的に手湾成できる。For example, by arrangement V# of A tree and 0411II, the third
The nitrifying solution circulation method as shown in Figures (a) and 3(b), or the non-circulating method as shown in Figures 3(c) and 3(d),
e), the ardenpho method as shown in FIG. 3(f) can be freely and selectively constructed.
このようにＡ槽と○槽の容量比ならびに配置を自由に変
更することにより、Ａ槽は活性汚泥の沈澱堆積および短
絡流が生じない程度の省エネルギー的無酸素攪拌を、該
攪拌様の回軒数制御により達する。In this way, by freely changing the capacity ratio and arrangement of tanks A and ○, tank A can perform energy-saving, oxygen-free stirring to the extent that activated sludge sedimentation and short-circuit flow will not occur, and the number of times of stirring can be adjusted. Reached through control.
実施例は第４図に示すように１１個に仕切られた生物反
応槽の各セルに嫌気・好気両用水中攪４１！磯が空気配
管を伴って設置され、Ａ槽と０槽の容量比並びに配置を
自由に変更し得る嫌気・好気活性汚泥処理装置を形成し
、処理条件に応じて流入側ａから順にＡ、Ａ、Ａ、Ｏ，
○、Ｏ，Ｏ，Ａ、Ａ、Ａ、０として脱窒、脱燐処理が行
なわれ、表−１に示すように極めて良好な処理水質が得
られている。又、この処理における機器の消費電力量を
表−２に示す。In this embodiment, as shown in Fig. 4, each cell of a biological reaction tank partitioned into 11 cells is equipped with both anaerobic and aerobic underwater stirring 41! A rock is installed with air piping to form an anaerobic/aerobic activated sludge treatment device in which the capacity ratio and arrangement of tanks A and 0 can be freely changed. A, A, O,
Denitrification and dephosphorization treatments were carried out as O, O, O, A, A, A, 0, and extremely good treated water quality was obtained as shown in Table 1. Table 2 shows the amount of power consumed by the equipment in this process.
ここで、用いられた嫌気・好気両用水中攪拌様は、目詰
まりを全（生ずることなく空気のｗＩｊｌｌＩＩ気泡化
を促す気泡面転翼には揚水攪拌と空気破砕の２つの機能
を具備しており、これらが同時に達成せられるように空
気は回転翼の下（上流側）に供給するよう設計されてい
るので、空気が供給された場合は機内水路に気泡の上昇
力が作用し、回転翼に掛ける揚水抵抗が軽減される結果
、好気攪拌時の消費電力は表−２からも明らかなように
著しく減少する特徴を有している。Here, the anaerobic/aerobic underwater agitation system used was designed to completely eliminate clogging and promote air bubbling without causing clogging.The bubbling blade has two functions: pumping water agitation and air crushing. The design is such that air is supplied below the rotor blades (on the upstream side) so that these can be achieved at the same time, so when air is supplied, the upward force of the bubbles acts on the in-flight waterway, causing the rotor blades to rise. As a result of the reduced pumping resistance, the power consumption during aerobic agitation is significantly reduced, as is clear from Table 2.
そして、空気の供給が遮断された無酸素（ｆｉ気）攪拌
では上記の作用がないので動力減少は起こらない。In anoxic (fi-air) stirring in which the supply of air is cut off, the above effect does not occur, so no reduction in power occurs.
本実施例に於いても他の全ての活性汚泥処理における攪
件故気装置同様に、機器選定に当たっては、好気処理に
要する酸素量を満足し得る能力が基準となっており、そ
の基準に照らして上記容量（表−２の定格動力値）のも
のが採用されている。In this example, as in all other activated sludge treatment agitated waste air systems, equipment selection was based on the ability to satisfy the amount of oxygen required for aerobic treatment; In light of this, the one with the above capacity (rated power value in Table 2) is adopted.
そしてこの時点では回転数制御を行わない一定速の運転
でありながら、同−機種であっても嫌気攪拌と好気攪拌
とでは、消費電力量に差異が生じているのは上記理由に
よっている。そして、通常攪拌様の運転と酸素移動との
関係は次のようになる。The above reason is why there is a difference in power consumption between anaerobic agitation and aerobic agitation even if the machine is of the same model, even though the machine is operating at a constant speed without any rotational speed control at this point. The relationship between normal stirring-like operation and oxygen transfer is as follows.
■−一定速運転し、空気の供給を遮断すれば酸素の移動
はなく、攪拌動力と攪拌強度は一定である。(2) If the device is operated at a constant speed and the air supply is cut off, there will be no movement of oxygen, and the stirring power and stirring intensity will remain constant.
■−一定速運転し、空気の供給を行えば、供給された空
気の量に応じて酸素移動量、並びに攪拌動力と攪拌強度
は変動する。(2) If the device is operated at a constant speed and air is supplied, the amount of oxygen transferred, as well as the stirring power and intensity will vary depending on the amount of supplied air.
実施例では当初、攪拌強度と生物反応の関係に対する知
見が充分でなかったことと、活性汚泥の沈澱および異物
等による攪拌障害防止の観点のみから、あえて好気攪拌
時に使用する高速の電動機をそのままの能力で嫌気攪拌
にも使用したため、表−２に示すとおり嫌気攪拌時の消
費電力量が最も多くなったものである。Initially, in the example, the high-speed electric motor used during aerobic agitation was intentionally used as is, because there was insufficient knowledge about the relationship between agitation intensity and biological reactions, and only from the perspective of preventing agitation failures due to activated sludge sedimentation and foreign matter. Since it was also used for anaerobic stirring with a capacity of
従って省エネルギーの観点からは、主としてＡ槽におけ
る攪拌動力低減を図るための調査、研究ならびに対策が
中心であることは明らかである。Therefore, from the perspective of energy conservation, it is clear that investigations, research, and measures to reduce the stirring power in tank A are the main focus.
攪拌動力と攪拌強度は電動機の回転数の′Ｘ乗に比例し
、？Ｉｆ勤磯の回転数は電源周波数に正比例する。The stirring power and stirring intensity are proportional to the number of rotations of the electric motor to the power of 'X', and ? If the rotation speed of the engine is directly proportional to the power supply frequency.
そこで既存の設備に改造を加えることなく該攪拌機の攪
拌強度を変え得る方法として周波数変換器を該攪拌の電
源（操作ｍ）に装着し、ダイヤルを手動操作して無段階
任意の回転数（攪拌強度）が得られるようにし、更にＡ
ＷＩの底部には活性汚泥の濃度変化を探知するべくＭＬ
ＳＳセンサーを設置して槽内盈視装置となし、生物反応
速度を低下させず、かつ活性汚泥の沈澱を生じない範囲
で、どの程度まで回転数（攪拌強度）を下げ得るかを実
態調査によってその結果を得るに至った。Therefore, as a method to change the stirring intensity of the stirrer without modifying the existing equipment, a frequency converter is attached to the stirring power supply (operation strength), and further A
ML is installed at the bottom of the WI to detect changes in the concentration of activated sludge.
An SS sensor was installed to act as an in-tank observation device, and a field survey was conducted to determine to what extent the rotation speed (agitation intensity) could be lowered without reducing the biological reaction rate and without causing activated sludge sedimentation. I got the result.
尚、本実態調査に用いた主な設備は次の通りである。The main equipment used in this survey is as follows.
嫌気槽容量 ２８５［ｍ２／セル］＝幅６．８［＋耐×
艮０．８［ｍｌＸ水深６［＋ａ］
攪拌様仕様 定格５．５［ｋｗ］、４ｒ’ ６０［ｌ１
ｚ１．回転数１９２［ｒ四１（減速機直結）
また、ある設定した周波数（周波数変換器使用）におけ
る攪拌所要動力、活性汚泥の分布状態、省エネルギー効
率および処理水′１１等の調査結果を表−３に示す。Anaerobic tank capacity 285 [m2/cell] = width 6.8 [+ resistance ×
0.8 [ml x water depth 6 [+a] Stirring specifications Rated 5.5 [kw], 4r' 60 [l1
z1. Number of revolutions: 192 [r41 (directly connected to reducer) Table 3 also shows the investigation results of the required stirring power, activated sludge distribution, energy saving efficiency, treated water '11, etc. at a certain set frequency (using a frequency converter). Shown below.
表−３に於いて、周波数変換器を操作することにより、
６０〜２２．３［Ｈｚｌまで大幅に攪拌強度を減少させ
ているにも拘らず、活性汚泥は適度の混合状態を維持し
ていることが判る。In Table 3, by operating the frequency converter,
It can be seen that the activated sludge maintains an appropriate mixed state even though the stirring intensity is significantly reduced to 60 to 22.3 Hzl.
２０［１１ｚｌにて上下に若干の濃度差の広がる傾向が
見られるので大体この辺りが限界がと推定されるが、安
全性を見込んで２５．５［１１ｚ ］をこの場合の最低
制御限界としても省エネルギー効率は実に８４．２［％
］にも達している。At 20[11zl, there is a tendency for the concentration difference to widen slightly above and below, so the limit is estimated to be around this area, but considering safety, we set 25.5[11z] as the minimum control limit in this case. Energy saving efficiency is actually 84.2%
] has also been reached.
また、この時の処理水質を見ても、除去対象とする窒素
、燐の残留濃度値は（ｉｏ［ＩＩｚ］（Ｉｉ！１１い攪
拌）ＩＬ？のそれ以下となっている。Also, looking at the quality of the treated water at this time, the residual concentration values of nitrogen and phosphorus to be removed are lower than that of (io[IIz] (Ii!11 stirring) IL?.
この￥Ｊ、験運転で下限基準とした２５．５［１１２１
時の嫌気攪拌消費電力量を表−２の場合に適用すると、
消費電力は、Ｗ＝０．８７［ｋｗ／台１×６［台］＝５
．２２［ｋｗｌで、回転数制御を行うことにより達する
省エネルギー効率は、
ｌへ＝＋（３３−５，２２）／３３１Ｘ１００＝８４．
２［％Ｊ好気攪拌も含めた全体では、
η＝［＋７４−（２３＋１８＋５．２２）ｌ／７４］Ｘ
ＩＱＱ＝３７．５［％１の省エネルギーとなる。This ¥J was 25.5[1121
If the power consumption of anaerobic stirring is applied to the case of Table 2,
Power consumption is W = 0.87 [kW/unit 1 x 6 [unit] = 5
．． The energy saving efficiency achieved by controlling the rotation speed at 22 kwl is: To l=+(33-5,22)/331X100=84.
2[%JIn total including aerobic stirring, η=[+74-(23+18+5.22)l/74]X
Energy saving of IQQ=37.5[%1].
処理性能面では、
■高速攪拌（強い攪拌）と低速攪拌（弱い攪拌）とでは
、生物反応速度は略同等か、もしくは弱い攪拌の方が若
干優位の傾向にある。In terms of treatment performance, ① The biological reaction rate is approximately the same with high-speed stirring (strong stirring) and low-speed stirring (weak stirring), or weak stirring tends to be slightly superior.
■極めて弱い攪拌の場合、Ａ槽表面にスカム層ができる
ことがあるが、スカム層がない場合よりも生物反応（脱
窒）は進む。■In the case of extremely weak agitation, a scum layer may form on the surface of tank A, but the biological reaction (denitrification) will progress more than if there was no scum layer.
■攪拌を全く停止しても汚泥界面下では、活性汚泥の濃
度に応じた脱窒速度をもっで脱窒が進行する。■Even if stirring is completely stopped, denitrification proceeds below the sludge interface at a denitrification rate that depends on the concentration of activated sludge.
以上より、攪拌強度そのものは生物反応速度と直接的に
は余りｔｘｌ係しないが、攪拌強度を強めるとＡ槽表面
の流れが強くなり、気液界面からの酸素溶は込みが多く
なる結果、”嫌気における生物反応”に必要な条件が悪
化する傾向を生むことが↑りる。Ａ槽における攪拌強度
は弱い方が処理性能は向上するとの結論に至り、処理性
能の向上と省エネルギーは完全に両立することがここに
見出だせたのである。From the above, the stirring intensity itself does not have much direct relation to the biological reaction rate, but as the stirring intensity increases, the flow on the surface of tank A becomes stronger, and as a result, the oxygen solution from the gas-liquid interface increases. The conditions necessary for anaerobic biological reactions tend to deteriorate. We came to the conclusion that treatment performance improves when the agitation intensity in tank A is weaker, and it was found here that improvement in treatment performance and energy saving are completely compatible.
但し、満足な処理水質を得るに必要な、”活性汚泥と被
処理水との充分な混合”を行うためには、活性汚泥の沈
澱や短絡流は避けなければならない。However, in order to achieve "sufficient mixing of activated sludge and water to be treated" necessary to obtain satisfactory treated water quality, sedimentation of activated sludge and short-circuit flow must be avoided.
従って、活性汚泥の濃度を探知（監視）し、常時、所要
最小攪拌強度を維持することがポイントになる。Therefore, it is important to detect (monitor) the concentration of activated sludge and maintain the required minimum stirring intensity at all times.
Ａ槽に於いてはＭＬＳＳセンサーが探知する活性汚泥Ｃ
度に連動して周波数変換器の自動制御可能なるよう電気
的に接続することにより、註攪拌磯の回転数を自動連続
制御する。In tank A, activated sludge C is detected by the MLSS sensor.
By electrically connecting the frequency converter to enable automatic control of the frequency converter, the rotational speed of the stirring rock can be automatically and continuously controlled.
また掻作盤にタイマーをセットして該変換器と電気的に
接続、連動させ、予め設定する周波数を自動間歇的に繰
り返し、時に応じて自動体止、自動再起動などの制御も
可能にする。In addition, by setting a timer on the scraping board and electrically connecting and interlocking it with the converter, the preset frequency can be automatically repeated intermittently, allowing controls such as automatic stop and automatic restart depending on the time. .
上記、自動連続制御、および自動間歇制御の夫々の場合
に応じて設けられる該変換器制御連絡回路を、ＯＦＦに
することにより任意手動繰作も可能である。Arbitrary manual operation is also possible by turning off the converter control communication circuit provided for each of the automatic continuous control and automatic intermittent control described above.
以上、嫌気・好気両用水中攪ｔｔ４Ｐ１による嫌気・好
気活性汚泥法を処理目的に応じて、硝化液循環法、非循
環法、Ｂ ａｒｄｅｎｐｈｏ法その他を使い分けるに当
たり、攪拌代の回転数を制御することは、単に省エネル
ギーのみならず、斯る汚水処理装置が最上使命とすると
ころの処理水質の向上と安定性を同時に達成する極めて
ｆｆ！要な事項を内在している。As mentioned above, when using the anaerobic/aerobic activated sludge method using anaerobic/aerobic underwater stirring tt4P1, the nitrification liquid circulation method, non-circulation method, Bardenpho method, etc. depending on the treatment purpose, the rotation speed of the stirring allowance should be controlled. This means that it not only saves energy, but also improves and stabilizes the quality of treated water, which is the ultimate mission of such sewage treatment equipment. Contains important matters.
〈発明の効果〉
本発明方法は、周波数変換器を用いて攪拌を蔑の回転数
を変換することにより、８′易に好気性攪拌或は嫌気性
攪拌の何れにも適した回転数を得られるので専用授（子
機である必要はなく、構成が簡単である。<Effects of the Invention> The method of the present invention can easily obtain a rotation speed suitable for either aerobic stirring or anaerobic stirring by converting the rotation speed for stirring using a frequency converter. Since it can be used as a dedicated terminal (it does not need to be a slave unit, the configuration is simple).
そして、上記のように処理法や、汚泥の種類、濃度等に
適した回転をすることができるので不適正な運転による
無駄な電力消費がなく、経費を節約することができる。As described above, since the rotation can be performed in a manner appropriate to the treatment method, type of sludge, concentration, etc., there is no wasted power consumption due to improper operation, and costs can be saved.
本発明方法によれば、酸素移動量に対する動力の利用効
率に優れ、常時３０〜４０（％）の省エネルギーとなり
、又、送気、断気何れの場合にも散気板、故気箭にこれ
まで発生したような目詰まりがみられず、性能を長期間
一定に保つことができるなど多くの優れた効果を有する
。According to the method of the present invention, the efficiency of using power with respect to the amount of oxygen transferred is excellent, and energy saving of 30 to 40% is achieved at all times. It has many excellent effects, such as no clogging that occurred in previous years, and the ability to maintain constant performance over a long period of time.
第１図は、本発明方法の実施例を示す処Ｊ”ｌ！槽の↑
＋ＹＩ成を側面図、
第２図（、）は、浅底処理槽の側面略図、第２図（ｂ）
は、深底処理槽の側面略図、第３図し）（＋１）は、硝
化液循環法の構成例を示す７０シート、
第３図（ｃ）（ｄ）は、非循環法の構成例を示す７０シ
ート、
第３図（ｅ）（ｆ）は、上記他の構成例を示す７０ン−
ト、
Ｐｔ５４図は、循環法による処ＪＴｌ￥槽の配置構成例
の７０シートの側面略図である。Figure 1 shows an example of the method of the present invention.
Figure 2 (,) is a side view of the +YI configuration, Figure 2 (a) is a schematic side view of the shallow treatment tank, Figure 2 (b)
3) (+1) is a 70 sheet showing an example of the configuration of the nitrification liquid circulation method, and Figures 3(c) and (d) are examples of the configuration of the non-circulation method. 70 sheets shown in FIG. 3(e) and (f) are 70 sheets showing other configuration examples above
Figure Pt54 is a schematic side view of 70 sheets of an example of the arrangement of a JTl tank for treatment using the circulation method.
Claims (1)
の生物反応槽の夫々の区分に嫌気・好気両用水中攪拌機
を設置して、嫌気槽或は好気槽の何れにも変換できるよ
うにすると共に、該嫌気槽と好気槽の容量比と配置何れ
をも自由に変更し得るようにして嫌気・好気活性汚泥処
理を可能にし、前記全攪拌機の内任意台数の攪拌強度を
、処理目的に照らし、嫌気槽を活性汚泥濃度に応じて、
自動連続的に、或は自動間歇的に、或は適宜手動操作で
制御するようにしたことを特徴とする水中攪拌機による
嫌気槽の運転制御方法。1. In the anaerobic/aerobic activated sludge method, an anaerobic/aerobic underwater agitator is installed in each section of multiple partitioned biological reaction tanks, so that neither the anaerobic tank nor the aerobic tank can be used. In addition, the capacity ratio and arrangement of the anaerobic tank and the aerobic tank can be freely changed to enable anaerobic/aerobic activated sludge treatment, and any number of agitators among the above-mentioned agitators can be used. The strength of the anaerobic tank is adjusted according to the treatment purpose and the activated sludge concentration.
A method for controlling the operation of an anaerobic tank using an underwater agitator, characterized in that the operation is controlled automatically continuously, automatically intermittently, or manually as appropriate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24895686A JPS63104699A (en) | 1986-10-20 | 1986-10-20 | Method for controlling operation of anaerobic tank by underwater stirrer |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24895686A JPS63104699A (en) | 1986-10-20 | 1986-10-20 | Method for controlling operation of anaerobic tank by underwater stirrer |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPS63104699A true JPS63104699A (en) | 1988-05-10 |
Family
ID=17185903
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24895686A Pending JPS63104699A (en) | 1986-10-20 | 1986-10-20 | Method for controlling operation of anaerobic tank by underwater stirrer |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS63104699A (en) |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2001009047A1 (en) * | 1999-08-02 | 2001-02-08 | Asio, S.R.O. | Municipal waste-water treatment method |
| KR100304058B1 (en) * | 1998-09-02 | 2001-11-22 | 이정국 | Reactor tank bulkhead and sewage treatment system used in sewage treatment system |
| KR100348528B1 (en) * | 1999-07-27 | 2002-08-14 | 주식회사 청우네이처 | Method and Apparatus of Biological Nutrient Removal for the Purification of Wastewater |
| JP2009131854A (en) * | 2009-03-23 | 2009-06-18 | Maezawa Ind Inc | Sewage treatment apparatus |
| JP2013212490A (en) * | 2011-11-08 | 2013-10-17 | Toshiba Corp | Nitrogen/phosphor removal treatment method and nitrogen/phosphor removal treatment apparatus |
| JP2017080667A (en) * | 2015-10-27 | 2017-05-18 | 住友重機械エンバイロメント株式会社 | Agitation system and water treatment equipment |
| JP2017094305A (en) * | 2015-11-27 | 2017-06-01 | 住友重機械エンバイロメント株式会社 | Agitation system |
| US10384963B2 (en) | 2015-03-25 | 2019-08-20 | Xylem Europe Gmbh | Method for controlling a treatment apparatus arrangement, a treatment apparatus arrangement for a treatment plant as well as a treatment plant |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5537959A (en) * | 1978-09-11 | 1980-03-17 | Tokyo Shibaura Electric Co | Control rod drive mechanism |
-
1986
- 1986-10-20 JP JP24895686A patent/JPS63104699A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5537959A (en) * | 1978-09-11 | 1980-03-17 | Tokyo Shibaura Electric Co | Control rod drive mechanism |
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100304058B1 (en) * | 1998-09-02 | 2001-11-22 | 이정국 | Reactor tank bulkhead and sewage treatment system used in sewage treatment system |
| KR100348528B1 (en) * | 1999-07-27 | 2002-08-14 | 주식회사 청우네이처 | Method and Apparatus of Biological Nutrient Removal for the Purification of Wastewater |
| WO2001009047A1 (en) * | 1999-08-02 | 2001-02-08 | Asio, S.R.O. | Municipal waste-water treatment method |
| JP2009131854A (en) * | 2009-03-23 | 2009-06-18 | Maezawa Ind Inc | Sewage treatment apparatus |
| JP2013212490A (en) * | 2011-11-08 | 2013-10-17 | Toshiba Corp | Nitrogen/phosphor removal treatment method and nitrogen/phosphor removal treatment apparatus |
| US10384963B2 (en) | 2015-03-25 | 2019-08-20 | Xylem Europe Gmbh | Method for controlling a treatment apparatus arrangement, a treatment apparatus arrangement for a treatment plant as well as a treatment plant |
| JP2017080667A (en) * | 2015-10-27 | 2017-05-18 | 住友重機械エンバイロメント株式会社 | Agitation system and water treatment equipment |
| JP2017094305A (en) * | 2015-11-27 | 2017-06-01 | 住友重機械エンバイロメント株式会社 | Agitation system |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| JP4994265B2 (en) | Water treatment apparatus and water treatment method | |
| JPS63104699A (en) | Method for controlling operation of anaerobic tank by underwater stirrer | |
| CN108609728A (en) | A kind of system and control method using dissolved oxygen modified sewage sludge filamentary discharges | |
| CN201777962U (en) | Oxidation ditch system for processing sewage | |
| KR100935914B1 (en) | Advanced wastewater treatment apparatus with two stage reactor | |
| CN214270604U (en) | Single-power sewage treatment system and sewage treatment tank thereof | |
| CN212269592U (en) | Wig production sewage treatment plant | |
| CN110526397B (en) | （AO） 2 Integrated multistage sedimentation circulating reactor | |
| WO1986003734A1 (en) | Nitrification/denitrification of waste material | |
| CN210825614U (en) | （AO）2- -precipitation integrated multistage circulation reactor | |
| CN107963782B (en) | Biological contact oxidation reaction system with enhanced denitrification function | |
| JPH0461716B2 (en) | ||
| JPS607997A (en) | Process and apparatus for purifying filthy turbid water in anaerobic and aerobic treating tank using underwater stirring | |
| CN220300561U (en) | Automatic sewage denitrification and dephosphorization device of control | |
| CN215975171U (en) | Limited response aeration water pollution treatment system | |
| CN219546810U (en) | Sewage treatment plant of integral type MABR membrane | |
| CN216711838U (en) | High concentration waste water MBR integration integrated system | |
| CN219972006U (en) | Combined aeration device for magnetic biochemical process | |
| CN218810837U (en) | Automatic allocation type biological denitrification device for high-organic high-ammonia-nitrogen wastewater treatment | |
| JPH04193399A (en) | Operating method of aeration stirrer of single tank type anaerobic and aerobic activated sludge method | |
| CN221254225U (en) | High-efficient sewage denitrification dephosphorization processing system | |
| CN217600471U (en) | Integrated sewage treatment equipment | |
| CN215365079U (en) | Pump station with deodorization and silt deposit prevention functions | |
| CN221217513U (en) | Integrated treatment device for landfill leachate | |
| CN217148794U (en) | Sewage treatment integrated device with air as power source |