JPH0763711B2 - Wastewater treatment method - Google Patents
Wastewater treatment methodInfo
- Publication number
- JPH0763711B2 JPH0763711B2 JP61004638A JP463886A JPH0763711B2 JP H0763711 B2 JPH0763711 B2 JP H0763711B2 JP 61004638 A JP61004638 A JP 61004638A JP 463886 A JP463886 A JP 463886A JP H0763711 B2 JPH0763711 B2 JP H0763711B2
- Authority
- JP
- Japan
- Prior art keywords
- aeration
- liquid
- treatment tank
- inflow
- hydrogen donor
- 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
- 238000004065 wastewater treatment Methods 0.000 title claims description 6
- 238000005273 aeration Methods 0.000 claims description 29
- 239000007788 liquid Substances 0.000 claims description 24
- 239000000852 hydrogen donor Substances 0.000 claims description 16
- 239000010802 sludge Substances 0.000 claims description 16
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 16
- 239000002351 wastewater Substances 0.000 claims description 14
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 11
- 238000003756 stirring Methods 0.000 claims description 11
- 241000894006 Bacteria Species 0.000 claims description 9
- 239000006228 supernatant Substances 0.000 claims description 7
- 238000001556 precipitation Methods 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 230000007246 mechanism Effects 0.000 claims description 5
- 229910052757 nitrogen Inorganic materials 0.000 claims description 5
- 230000029058 respiratory gaseous exchange Effects 0.000 claims description 4
- 238000000926 separation method Methods 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 230000033116 oxidation-reduction process Effects 0.000 claims description 2
- 238000000034 method Methods 0.000 description 36
- 238000006243 chemical reaction Methods 0.000 description 21
- 230000008569 process Effects 0.000 description 16
- 238000001514 detection method Methods 0.000 description 10
- 239000005416 organic matter Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 6
- 230000008901 benefit Effects 0.000 description 3
- 230000008859 change Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 3
- QGZKDVFQNNGYKY-UHFFFAOYSA-N Ammonia Chemical compound N QGZKDVFQNNGYKY-UHFFFAOYSA-N 0.000 description 2
- 102000004190 Enzymes Human genes 0.000 description 2
- 108090000790 Enzymes Proteins 0.000 description 2
- GRYLNZFGIOXLOG-UHFFFAOYSA-N Nitric acid Chemical compound O[N+]([O-])=O GRYLNZFGIOXLOG-UHFFFAOYSA-N 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 2
- 241001148470 aerobic bacillus Species 0.000 description 2
- 239000001257 hydrogen Substances 0.000 description 2
- 229910052739 hydrogen Inorganic materials 0.000 description 2
- 229910017604 nitric acid Inorganic materials 0.000 description 2
- 230000000241 respiratory effect Effects 0.000 description 2
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 description 1
- 229910002651 NO3 Inorganic materials 0.000 description 1
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 1
- IOVCWXUNBOPUCH-UHFFFAOYSA-N Nitrous acid Chemical compound ON=O IOVCWXUNBOPUCH-UHFFFAOYSA-N 0.000 description 1
- 238000013019 agitation Methods 0.000 description 1
- 229910021529 ammonia Inorganic materials 0.000 description 1
- 230000001651 autotrophic effect Effects 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 229910001873 dinitrogen Inorganic materials 0.000 description 1
- 150000002431 hydrogen Chemical class 0.000 description 1
- 244000144972 livestock Species 0.000 description 1
- 230000000813 microbial effect Effects 0.000 description 1
- 239000011259 mixed solution Substances 0.000 description 1
- 150000002897 organic nitrogen compounds Chemical class 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 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】 A,産業上の利用分野 本発明は、排水中の有機物を微生物処理により分解する
ための排水処理方法に関するものである。The present invention relates to a wastewater treatment method for decomposing organic matter in wastewater by microbial treatment.
B,発明の概要 本発明方法は、有機性の排水を活性汚泥を用いた回分方
式により処理する方法において、 先ず好気処理を行い、次いで嫌気性条件下にて水素供与
体としての有機物を排水中に供給して嫌気処理を行い、
その後再び好気処理を行うことによつて、 高い脱窒効果を得るようにしたものである。B, Summary of the Invention The method of the present invention is a method of treating organic wastewater by a batch method using activated sludge, first performing aerobic treatment, and then draining organic matter as a hydrogen donor under anaerobic conditions. It is supplied inside and anaerobic treatment is performed.
After that, aerobic treatment is performed again to obtain a high denitrification effect.
C,従来の技術及び発明が解決しようとする問題点 最近において、小規模の排水処理施設を中心に回分式活
性汚泥法が注目されつつある。この方法は、処理槽内の
活性汚泥の混合液中に排水を流入し、ここで曝気、固液
分離及び上澄液排出を行う方法であり、バルキングが
発生しない、省エネルギー的である、高度な運転技
術を要しない等の利点がある。また通常の連続運転と比
較して、曝気、沈殿を繰り返すことから脱窒，脱リン効
果も高いといわれている。C, Problems to be Solved by Conventional Techniques and Inventions In recent years, the batch activated sludge method has been attracting attention mainly for small-scale wastewater treatment facilities. This method is a method in which wastewater flows into a mixed liquid of activated sludge in a treatment tank, where aeration, solid-liquid separation, and supernatant liquid discharge are performed, and bulking does not occur, energy saving, and advanced There are advantages such as not requiring driving skills. It is also said that the effect of denitrification and dephosphorization is higher than that of normal continuous operation because it repeats aeration and precipitation.
しかしながら回分式活性汚泥法において、脱窒効果が高
いといつてもそれは経験的な実証からいわれていること
であつて、実働させた場合常に良好な脱窒効果が得られ
るという保障には至つていない。However, in the batch activated sludge method, the high denitrification effect is always said from empirical evidence, and it cannot be guaranteed that a good denitrification effect will always be obtained when it is actually used. Not not.
本発明はこのような事情にもとづいてなされたものであ
り、従来の回分式の方法の利点を生かしながら、脱窒効
果の高い回分式の排水処理方法を提供することを目的と
するものである。The present invention has been made under such circumstances, and an object of the present invention is to provide a batch-type wastewater treatment method having a high denitrification effect while taking advantage of the advantages of the conventional batch-type method. .
D,問題点を解決するための手段及び作用 本発明の内容を説明する前に、先ず第４図によつて有機
性窒素化合物例えばタンパク質が硝化反応、脱窒反応を
経て分解されていく様子を示す。同図においてワクで囲
つた細菌は従属栄養細菌であり、他の細菌は独立栄養細
菌である。また点線矢印に対応する反応は好気性条件で
進行する硝化反応であり、鎖線矢印に対応する反応は嫌
気性条件で進行する脱窒反応である。脱窒反応を化学量
論的に表わすと次式のようになる。D, Means and Actions for Solving Problems Before explaining the contents of the present invention, first, referring to FIG. 4, a state in which an organic nitrogen compound such as a protein is decomposed through a nitrification reaction and a denitrification reaction is shown. Show. In the figure, the bacteria surrounded by wax are heterotrophic bacteria, and the other bacteria are autotrophic bacteria. The reaction corresponding to the dotted arrow is a nitrification reaction that proceeds under aerobic conditions, and the reaction corresponding to the chain arrow is a denitrification reaction that proceeds under anaerobic conditions. The denitrification reaction is stoichiometrically expressed as follows.
2NO2 -＋３（H2）→N2＋2OH-＋2H2O ……（１） 2NO3 -＋５（H2）→N2＋2OH-＋4H2O ……（２） ただし（１），（２）式は夫々亜硝酸呼吸及び硝酸呼吸
に相当するものである。これらの反応の（H2）は細菌内
の呼吸酵素系を経由して水素供与体から与えられるが、
脱窒菌のほとんどは有機物を水素供与体としている。 2NO 2 - +3 (H 2) → N 2 + 2OH - + 2H 2 O ...... (1) 2NO 3 - +5 (H 2) → N 2 + 2OH - + 4H 2 O ...... (2) provided that (1), (2) The equations correspond to nitrite respiration and nitrate respiration, respectively. (H 2 ) of these reactions is given from the hydrogen donor via the respiratory enzyme system in bacteria,
Most of the denitrifying bacteria use organic substances as hydrogen donors.
本発明はこのような点に着目してなされたものであり、
排水を処理槽内で好気性処理し、次いで有機物を含む水
素供与体液を処理槽内に導入して嫌気性処理を行い、そ
の後再び好気性処理を行うことによつて、残存している
有機物を分解するようにしたものである。The present invention has been made paying attention to such a point,
The wastewater is subjected to aerobic treatment in the treatment tank, then a hydrogen donor liquid containing organic matter is introduced into the treatment tank to perform anaerobic treatment, and then aerobic treatment is performed again to remove residual organic matter. It is designed to be disassembled.
具体的には本発明方法は、処理槽内の活性汚泥の混合液
中に排水を流入ポンプによつて流入する流入工程と、こ
の流入工程の後前記処理槽内を曝気手段により曝気する
第１の曝気工程と、次いで曝気を停止した後汚泥中の脱
窒菌の呼吸により上澄液中の窒素を除去するために、有
機物を含む水素供与体液を水素供与体液用のポンプによ
り処理槽内に供給すると共に、処理槽内を撹拌手段によ
り撹拌する混合工程と、この混合工程により混合された
混合液を曝気手段により曝気する第２の曝気工程と、そ
の後曝気を停止して固液分離を行う沈殿工程と、この沈
殿工程により分離された上澄液を処理水として排出機構
により排出する排出工程とから成り、 前記処理槽内には酸化還元電位検出部を設け、この検出
部よりの検出電位にもとづいて、制御部を介して前記曝
気手段、水素供与体液用のポンプ及び撹拌手段をオン／
オフ制御する方法である。Specifically, in the method of the present invention, an inflow step in which wastewater flows into a mixed liquid of activated sludge in a treatment tank by an inflow pump, and after this inflow step, aeration means aerates the inside of the treatment tank In order to remove nitrogen in the supernatant liquid by the aeration process of the above and then by breathing denitrifying bacteria in the sludge after stopping the aeration, the hydrogen donor liquid containing organic substances is supplied into the treatment tank by the hydrogen donor liquid pump. In addition, a mixing step in which the inside of the treatment tank is stirred by the stirring means, a second aeration step in which the mixed solution mixed in this mixing step is aerated by the aeration means, and then aeration is stopped to perform solid-liquid separation. And a discharge step of discharging the supernatant liquid separated by this precipitation step as treated water by a discharge mechanism. An oxidation-reduction potential detection section is provided in the treatment tank, and a detection potential from this detection section is set. Based on Turn on / off the aeration means, the pump for the hydrogen donor liquid, and the stirring means via the control unit.
This is a method of off control.
E,実施例 以下本発明方法の実施例を説明する。第１図は本発明を
実施する装置の一例を示す縦断面図、第２図は実施例の
方法を示す工程図である。第１図中１は処理槽、２は流
入ポンプ、Ｂはブロワ、３は散気手段、４は撹拌機、Ｍ
はモータであり、処理槽１内には予め活性汚泥の混合液
がベース水位B.W.Lまで収容されている。この例ではブ
ロワＢ及び散気手段３により曝気手段が構成され、撹拌
機４及びモータＭにより撹拌手段が構成される。実施例
においては、例えば畜舎排水等の高濃度有機性排水（以
下「原水」という。）を予め希釈あるいは嫌気処理した
排水を、先ず処理槽１内の上限水位レベルH.W.Lまで流
入させ、撹拌機４により撹拌し、これにより排水と活性
汚泥とを十分混合する。なお流入工程によつて十分混合
する場合には撹拌工程は不要である。次にブロワＢを駆
動して散気手段３より空気を放出し、これにより処理槽
１内を所定時間曝気する。この曝気工程によつて、活性
汚泥中の好気性菌群による好気処理が行われ、排水中の
有機物から分解し、硝化反応が進行する。そして十分に
曝気した後即ち有機物が十分除去され、硝化が十分行わ
れた後、曝気を停止し、汚泥を沈殿させる。この沈殿工
程によつて沈殿汚泥が嫌気条件下になつてから、水素供
与体液用のポンプ５を駆動することによつて例えば原水
を適量間欠的に処理槽１内に流入し、撹拌手段４で撹拌
して原水中の有機物と汚泥分と上澄液とを混合する。な
お原水の流入工程及び撹拌工程は混合工程をなすもので
ある。ここで原水を流入させるのは次に述べる水素供与
体としての有機物を補充するためである。そして汚泥中
の脱窒菌は、撹拌工程中に呼吸酵素系を経由して有機物
から水素を取り出し、この水素と前記曝気工程で生成さ
れた硝酸及び亜硝酸中の窒素とを反応させて当該窒素を
窒素ガスに還元して除去する。その後再び曝気を行い、
好気性菌群によつて、残存している有機物を除去すると
共にアンモニア成分を硝化し、次いで曝気を停止して汚
泥分を沈殿させる。その後排出機構６によつて処理槽１
の上澄液を排出する。E, Example Hereinafter, an example of the method of the present invention will be described. FIG. 1 is a longitudinal sectional view showing an example of an apparatus for carrying out the present invention, and FIG. 2 is a process drawing showing the method of the embodiment. In FIG. 1, 1 is a processing tank, 2 is an inflow pump, B is a blower, 3 is an air diffusing means, 4 is a stirrer, and M.
Is a motor, and the mixed liquid of activated sludge is previously stored in the treatment tank 1 up to the base water level BWL. In this example, the blower B and the air diffusing unit 3 constitute an aeration unit, and the stirrer 4 and the motor M constitute a stirring unit. In the embodiment, for example, a high-concentration organic wastewater (hereinafter referred to as “raw water”) such as livestock wastewater is diluted or anaerobically treated, and the wastewater is first allowed to flow up to the upper limit water level HWL in the treatment tank 1, and then the agitator 4 is operated. And the wastewater and activated sludge are mixed well. Note that the stirring step is not necessary when the mixing is sufficiently performed by the inflow step. Next, the blower B is driven to release the air from the air diffusing means 3, whereby the inside of the processing tank 1 is aerated for a predetermined time. By this aeration process, aerobic treatment is carried out by the aerobic bacteria group in the activated sludge, the organic matter in the waste water is decomposed, and the nitrification reaction proceeds. After sufficient aeration, that is, after sufficient removal of organic substances and sufficient nitrification, aeration is stopped and sludge is precipitated. After the sludge settled under the anaerobic condition by this settling step, by driving the pump 5 for the hydrogen donor liquid, for example, an appropriate amount of raw water intermittently flows into the treatment tank 1, and the stirring means 4 Stir to mix the organic matter in the raw water, the sludge and the supernatant. The raw water inflow process and the stirring process constitute a mixing process. The raw water is introduced here to replenish the organic matter as the hydrogen donor described below. Then, the denitrifying bacteria in the sludge take out hydrogen from the organic matter via the respiratory enzyme system during the stirring process, and react this hydrogen with the nitrogen in the nitric acid and nitrite generated in the aeration process to remove the nitrogen. Reduce to nitrogen gas and remove. After that, aeration is performed again,
Depending on the aerobic bacteria group, the remaining organic substances are removed and the ammonia component is nitrified, and then aeration is stopped to precipitate sludge. After that, by the discharge mechanism 6, the processing tank 1
Drain the supernatant.
本発明では、こうした一連の工程のシーケンス制御を、
処理槽１の酸化還元電位（以下「ORP」という。）にも
とづいて行うようにしている。第１図中７はORP検出部
であり、例えば故障等に対応するために３個のORP計よ
り成る。各ORP計よりのORPの検出値は選定回路８に入力
されここで適正値が選定される。選定された検出値は、
比較部91及び92より成る制御部９に入力され、先ず比較
部91にて、BOD除去反応、硝化反応及び脱窒反応に夫々
対応する設定値と比較され、その比較結果にもとづいて
指令部92を介してポンプ2,5、ブロワＢ、モータＭ及び
排出機構をオン／オフ制御する。In the present invention, the sequence control of such a series of steps,
The processing is performed based on the redox potential of the processing tank 1 (hereinafter referred to as "ORP"). Reference numeral 7 in FIG. 1 denotes an ORP detector, which is composed of three ORP meters in order to cope with a failure or the like. The ORP detection value from each ORP meter is input to the selection circuit 8 where an appropriate value is selected. The selected detection value is
The data is input to the control unit 9 including the comparison units 9 1 and 9 2 , and firstly, the comparison unit 9 1 compares the set values corresponding to the BOD removal reaction, the nitrification reaction and the denitrification reaction, respectively, and based on the comparison result. pump 2,5 via the command unit 9 2, blower B, and on / off control of the motor M and the discharge mechanism.
第３図の実線（イ）は本発明方法の各工程とORPの検出
値との関係を示すグラフであり、点線（ロ）は通常の回
分法（流入工程、曝気工程、沈殿工程及び排出工程より
成る方法）の各工程とORPの検出値との関係を示すグラ
フである。なお第３図の実験結果を得るにあたつて、被
処理水としては、BODが2000mg/程度の高濃度有機性排
水を嫌気性濾床法により嫌気処理したものを用いてお
り、水素供与体液としては嫌気処理を行つていない高濃
度有機性排水を用いている。The solid line (a) in FIG. 3 is a graph showing the relationship between each step of the method of the present invention and the detected value of ORP, and the dotted line (b) is a normal batch method (inflow step, aeration step, precipitation step and discharge step). Is a graph showing the relationship between each step of the method (1) and the detected value of ORP. In obtaining the experimental results shown in Fig. 3, as the water to be treated, high-concentration organic wastewater with a BOD of about 2000 mg / was anaerobically treated by the anaerobic filter bed method. For this, high-concentration organic wastewater that has not undergone anaerobic treatment is used.
ところで例えばAg/Agcl電極で測定したORPについては、
BOD除去反応が＋100〜＋200mV、硝化反応が＋250〜＋35
0mV、脱窒反応が−250〜−300mV程度で夫々作用すると
いわれている。このようなことにもとづいて各反応が進
行しやすいORPの範囲を把握し、その範囲を第２図のＩ
〜IIIとして示す。Ｉは硝化反応、IIはBOD除去反応、II
Iは脱窒反応が夫々進行しやすいORPの範囲である。本発
明では、これらORPの範囲と検出値とを照らし合わせる
ことによつて、各工程の開始及び終了のタイミングをと
るようにしており、具体的には例えばはじめの曝気工程
でORPの検出値が＋300mV程度になつたときに曝気手段を
オフして沈殿工程を開始し、また原水の流入工程におい
ては、ORPの検出値が−250mV程度になるように原水供給
量を制御し、再び曝気する工程においては、ORPの検出
値が＋150mV程度になつたときに曝気手段をオフするよ
うにしている。第２図のグラフ（イ）からわかるよう
に、原水流入工程にてORP値の大幅な変化が観察でき、
シーケンス制御を行うにあたつては、通常の回分法にて
ORPを指標とする場合よりも本発明方法にてORPを指標と
する場合の方が有効である。By the way, for example, for ORP measured with Ag / Agcl electrodes,
BOD removal reaction is +100 to +200 mV, nitrification reaction is +250 to +35
It is said that 0 mV and a denitrification reaction act at about -250 to -300 mV respectively. Based on this, the range of ORP in which each reaction is likely to proceed is grasped, and the range is shown in FIG.
~ III. I is nitrification reaction, II is BOD removal reaction, II
I is the range of ORP in which the denitrification reaction easily progresses. In the present invention, by comparing the range of these ORP and the detection value, the timing of the start and end of each step is taken, specifically, for example, the detection value of ORP in the first aeration step is The aeration means is turned off to start the precipitation process when it reaches about +300 mV, and in the inflow process of raw water, the amount of raw water supply is controlled so that the ORP detection value is about -250 mV, and aeration is performed again. In, the aeration means is turned off when the ORP detection value reaches about +150 mV. As can be seen from the graph (a) in Fig. 2, a significant change in the ORP value can be observed in the raw water inflow process,
When performing sequence control, use the normal batch method.
It is more effective to use ORP as an index in the method of the present invention than to use ORP as an index.
以上において各工程のシーケンス制御をタイマーにより
行うことも可能であるが、この場合には排水の状態や流
入量等の流入特性が変化しても一律の制御が行われるの
で良好な処理を行えないこともある。これに対してORP
値を指標としてシーケンス制御を行えば、流入特性に応
じて各工程の時間を調整できるから、常に安定した処理
を行うことができる。In the above, it is possible to perform sequence control of each process by a timer, but in this case uniform control is performed even if the inflow characteristics such as the drainage state and the inflow amount change, so good processing cannot be performed. Sometimes. On the other hand, ORP
If the sequence control is performed using the value as an index, the time of each process can be adjusted according to the inflow characteristics, so that stable processing can always be performed.
なお、本発明では、原水を流入した後曝気してから、再
び原水を流入して脱窒反応を進行させてもよい。In the present invention, the raw water may be introduced and then aerated, and then the raw water may be introduced again to allow the denitrification reaction to proceed.
F,発明の効果 以上のように本発明によれば、先ず好気処理を行い、次
いで嫌気性条件にて水素供与体としての有機物を排水中
に供給して嫌気処理を行い、その後再び好気処理を行う
ようにしたいわば２段回分法を採用しているため、好気
処理により生成した硝酸や亜硝酸中の窒素が嫌気処理に
よつて十分に除去されると共に、嫌気処理後に残存して
いる有機物は次段の好気処理にて分解されるので、良好
な排水処理を行うことができる。このため嫌気処理の際
の水素供与体液として原水を用いることができるから、
そうすることによつてランニングコストを抑えることが
できる。そして水素供与体液の混合工程や曝気工程等の
スケジユール管理をORPの検出値にもとづいて行つてい
るから、先述したように流入特性が変動しても安定した
処理を行うができる。F, Effect of the Invention As described above, according to the present invention, first, aerobic treatment is performed, then, under anaerobic conditions, an organic substance as a hydrogen donor is supplied into wastewater to perform anaerobic treatment, and then aerobic treatment is performed again. Since the so-called two-stage batch method is adopted so that nitric acid and nitrogen in nitrous acid produced by aerobic treatment are sufficiently removed by anaerobic treatment and remain after anaerobic treatment. Since the organic matter existing therein is decomposed in the subsequent aerobic treatment, good wastewater treatment can be performed. Therefore, raw water can be used as the hydrogen donor liquid in the anaerobic treatment,
By doing so, running costs can be reduced. Since the schedule control such as the mixing process of the hydrogen donor liquid and the aeration process is performed based on the detected value of ORP, stable processing can be performed even if the inflow characteristics change as described above.
第１図は本発明方法を実施する装置の一例を示す構成
図、第２図は本発明の実施例を示す工程図、第３図は酸
化還元電位の経時変化を示すグラフ、第４図は硝化，脱
窒反応を示す模式図である。 １……処理槽、２……流入ポンプ、３……散気手段、４
……撹拌手段、５……水素供与体液用のポンプ、６……
排出機構、７……酸化還元電位検出部、９……制御部。FIG. 1 is a configuration diagram showing an example of an apparatus for carrying out the method of the present invention, FIG. 2 is a process diagram showing an embodiment of the present invention, FIG. 3 is a graph showing changes with time of redox potential, and FIG. It is a schematic diagram which shows nitrification and a denitrification reaction. 1 ... Treatment tank, 2 ... Inflow pump, 3 ... Air diffuser, 4
...... Agitation means, 5 ...... Pump for hydrogen donor liquid, 6 ......
Ejection mechanism, 7 ... Redox potential detection unit, 9 ... Control unit.
Claims (1)
入ポンプによつて流入する流入工程と、この流入工程の
後前記処理槽内を曝気手段により曝気する第１の曝気工
程と、次いで曝気を停止した後、汚泥中の脱窒菌の呼吸
により上澄液中の窒素を除去するために、有機物を含む
水素供与体液を水素供与体液用のポンプにより処理槽内
に供給すると共に、処理槽内を撹拌手段により撹拌する
混合工程と、この混合工程により混合された混合液を曝
気手段により曝気する第２の曝気工程と、その後曝気を
停止して固液分離を行う沈殿工程と、この沈殿工程によ
り分離された上澄液を処理水として排出機構により排出
する排出工程とを含み、 前記処理槽内には酸化還元電位検出部を設け、この検出
部よりの検出電位にもとづいて、制御部を介して前記曝
気手段、水素供与体液用のポンプ及び撹拌手段をオン／
オフ制御することを特徴とする排水処理方法。1. An inflow step in which wastewater flows into a mixed liquid of activated sludge in a treatment tank by an inflow pump, and a first aeration step in which the inside of the treatment tank is aerated by an aeration means after this inflow step. Then, after stopping the aeration, in order to remove nitrogen in the supernatant liquid by respiration of denitrifying bacteria in the sludge, a hydrogen donor liquid containing organic substances is supplied into the treatment tank by a pump for the hydrogen donor liquid, A mixing step of stirring the inside of the treatment tank by a stirring means, a second aeration step of aerating the mixed liquid mixed by this mixing step by an aeration means, and a precipitation step of subsequently stopping aeration and performing solid-liquid separation, Including a discharge step of discharging the supernatant liquid separated by the precipitation step as a treated water by a discharge mechanism, an oxidation-reduction potential detector is provided in the treatment tank, based on the detected potential from the detector, Via control Turn on / off the aeration means, the hydrogen donor liquid pump, and the stirring means.
Wastewater treatment method characterized by off control.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61004638A JPH0763711B2 (en) | 1986-01-13 | 1986-01-13 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP61004638A JPH0763711B2 (en) | 1986-01-13 | 1986-01-13 | Wastewater treatment method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS62163798A JPS62163798A (en) | 1987-07-20 |
| JPH0763711B2 true JPH0763711B2 (en) | 1995-07-12 |
Family
ID=11589540
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP61004638A Expired - Lifetime JPH0763711B2 (en) | 1986-01-13 | 1986-01-13 | Wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0763711B2 (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100332496B1 (en) * | 1999-05-24 | 2002-04-17 | 채문식 | Method and Apparatus of denitrification for the purification of wastewater by using reduction of electric energy |
| JP5717187B2 (en) * | 2010-03-15 | 2015-05-13 | メタウォーター株式会社 | Waste water treatment method and waste water treatment equipment |
Family Cites Families (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5784793A (en) * | 1980-11-14 | 1982-05-27 | Ebara Infilco Co Ltd | Denitrification of organic waste water |
| JPS5784792A (en) * | 1980-11-14 | 1982-05-27 | Ebara Infilco Co Ltd | Denitrification of organic waste water |
| JPS5990695A (en) * | 1982-11-15 | 1984-05-25 | Mitsubishi Heavy Ind Ltd | Treatment of waste water |
-
1986
- 1986-01-13 JP JP61004638A patent/JPH0763711B2/en not_active Expired - Lifetime
Also Published As
| Publication number | Publication date |
|---|---|
| JPS62163798A (en) | 1987-07-20 |
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