JPH11188365A - Sewage treatment apparatus - Google Patents

Sewage treatment apparatus

Info

Publication number
JPH11188365A
JPH11188365A JP9358797A JP35879797A JPH11188365A JP H11188365 A JPH11188365 A JP H11188365A JP 9358797 A JP9358797 A JP 9358797A JP 35879797 A JP35879797 A JP 35879797A JP H11188365 A JPH11188365 A JP H11188365A
Authority
JP
Japan
Prior art keywords
sewage
electrodes
storage tank
electrode
treatment apparatus
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.)
Granted
Application number
JP9358797A
Other languages
Japanese (ja)
Other versions
JP3796033B2 (en
Inventor
Masaki Moriizumi
雅貴 森泉
Akihiro Fukumoto
明広 福本
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Sanyo Electric Co Ltd
Original Assignee
Sanyo Electric Co Ltd
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Sanyo Electric Co Ltd filed Critical Sanyo Electric Co Ltd
Priority to JP35879797A priority Critical patent/JP3796033B2/en
Priority to TW087119085A priority patent/TW442444B/en
Priority to KR1019980055179A priority patent/KR100293311B1/en
Priority to CN98125540A priority patent/CN1220975A/en
Publication of JPH11188365A publication Critical patent/JPH11188365A/en
Application granted granted Critical
Publication of JP3796033B2 publication Critical patent/JP3796033B2/en
Anticipated expiration legal-status Critical
Expired - Lifetime legal-status Critical Current

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Classifications

    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/463—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis by electrocoagulation
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
    • C02F1/461—Treatment of water, waste water, or sewage by electrochemical methods by electrolysis
    • C02F1/46104—Devices therefor; Their operating or servicing
    • C02F1/46109—Electrodes
    • C02F2001/46133—Electrodes characterised by the material
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4612—Controlling or monitoring
    • C02F2201/46125—Electrical variables
    • C02F2201/4613—Inversing polarity
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4612—Controlling or monitoring
    • C02F2201/46125—Electrical variables
    • C02F2201/4614—Current
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2201/00—Apparatus for treatment of water, waste water or sewage
    • C02F2201/46—Apparatus for electrochemical processes
    • C02F2201/461—Electrolysis apparatus
    • C02F2201/46105—Details relating to the electrolytic devices
    • C02F2201/4612—Controlling or monitoring
    • C02F2201/46145—Fluid flow
    • 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

  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Electrochemistry (AREA)
  • General Chemical & Material Sciences (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Organic Chemistry (AREA)
  • Water Treatment By Electricity Or Magnetism (AREA)
  • Treatment Of Biological Wastes In General (AREA)
  • Activated Sludge Processes (AREA)
  • Removal Of Specific Substances (AREA)

Abstract

PROBLEM TO BE SOLVED: To provide a sewage treatment apparatus which removes phosphoric acid in sewage stably by preventing the passivation of insoluble phosphate forming metal ions when the ion s are eluted electrochemically into sewage and can prevent the elevation of the voltage between electrodes. SOLUTION: A sewage treatment apparatus D1 is equipped with a sewage housing tank, four sets of iron electrodes in the tank, and a direct current power source 126 and incorporated into a small-sized combination treatment purification tank 101. The power source 126 supplies the current for electrolysis. A control part 125 removes phosphoric acid in sewage stably by preventing the passivation of iron ions when the ions are eluted from the electrodes and prevents the elevation of the voltage between electrodes a to control the current density of electrolysis to be kept always at 0.1-5.0 mA/cm<2> for constant current electrolysis and polarity inversion to be indicated once every 30 min-5 days.

Description

【発明の詳細な説明】DETAILED DESCRIPTION OF THE INVENTION

【０００１】[0001]

【発明の属する技術分野】本発明は汚水処理装置に関
し、さらに詳しくは、屎尿廃水や生活廃水などの汚水に
含まれるリン酸を電気分解により溶出した金属イオンと
反応させて除去するための汚水処理装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a sewage treatment apparatus, and more particularly to a sewage treatment apparatus for removing phosphoric acid contained in sewage such as human wastewater or domestic wastewater by reacting with metal ions eluted by electrolysis. Related to the device.

【０００２】[0002]

【従来の技術】この種の汚水処理装置としては、従来、
次のようなものが知られている。2. Description of the Related Art Conventionally, this type of sewage treatment apparatus
The following are known.

【０００３】すなわち、処理すべき汚水が収納される汚
水収納槽を設け、その槽内に不溶性リン酸塩形成金属か
らなる電極を一組以上配置しておき、これらの電極間に
電圧を印加して電気化学的に水不溶性リン酸塩形成金属
イオンを汚水中に溶出させることで、リン酸を水不溶性
リン酸塩にして沈殿除去するようにした装置である。That is, a sewage storage tank for storing sewage to be treated is provided, one or more pairs of electrodes made of an insoluble phosphate-forming metal are arranged in the tank, and a voltage is applied between these electrodes. This is an apparatus for electrochemically dissolving water-insoluble phosphate-forming metal ions into sewage to convert phosphoric acid into a water-insoluble phosphate for precipitation and removal.

【０００４】[0004]

【発明が解決しようとする課題】このような汚水処理装
置においては、場合により、電極の表面に不動態皮膜と
よばれる耐蝕性酸化皮膜が形成される結果、水不溶性リ
ン酸塩形成金属イオンの溶出が減少したり停止したりす
るおそれがある（不動態化）。このような不動態化が起
こると、汚水中のリン酸を水不溶性リン酸塩にして除去
することが困難になったり不可能になったりする。In such a sewage treatment apparatus, in some cases, a corrosion-resistant oxide film called a passive film is formed on the surface of the electrode, and as a result, water-insoluble phosphate-forming metal ions are formed. Elution may decrease or stop (passivation). When such passivation occurs, it becomes difficult or impossible to remove the phosphoric acid in the wastewater into a water-insoluble phosphate.

【０００５】また、場合により、電極間電圧が高くなり
すぎて消費電力が増大するおそれがある。[0005] In some cases, the voltage between the electrodes may be too high and power consumption may increase.

【０００６】本発明は、このような実情に鑑みてなされ
たものであり、汚水中に水不溶性リン酸塩形成金属イオ
ンを電気化学的に溶出させる際の不動態化を防止して、
汚水中のリン酸を安定的に除去するとともに、電極間電
圧の上昇を防止することのできる汚水処理装置を提供す
ることを課題とする。The present invention has been made in view of such circumstances, and has been made to prevent the passivation of a water-insoluble phosphate-forming metal ion from being electrochemically eluted into wastewater,
An object of the present invention is to provide a sewage treatment apparatus capable of stably removing phosphoric acid in sewage and preventing an increase in voltage between electrodes.

【０００７】[0007]

【課題を解決するための手段】本発明によれば、汚水収
納槽と、この汚水収納槽に配され、その汚水中のリン酸
を沈殿除去するための鉄イオンまたはアルミニウムイオ
ンを電気分解により溶出する少なくとも一組の電極と、
この電極に電解用電流を供給するための電源と、電極に
おける電流密度を不動態皮膜の生成が防止できるように
かつ電極間電圧の上昇を防止できるように制御する制御
部とを備えてなることを特徴とする汚水処理装置が提供
される。According to the present invention, a waste water storage tank and an iron ion or aluminum ion disposed in the waste water storage tank for precipitating and removing phosphoric acid in the waste water are eluted by electrolysis. At least one set of electrodes,
A power supply for supplying a current for electrolysis to the electrode, and a control unit for controlling a current density in the electrode so as to prevent generation of a passive film and to prevent an increase in inter-electrode voltage. The present invention provides a sewage treatment apparatus characterized by the following.

【０００８】汚水収納槽は、電気分解処理に供される汚
水が収納される。電極は、例えば長方形板状のものが２
枚一組で所定組配され、電気分解により鉄イオンまたは
アルミニウムイオンを汚水収納槽に溶出させる。電源
は、各組の電極に電気分解のための電流を供給する。The sewage storage tank stores sewage to be subjected to electrolysis. The electrodes are, for example, rectangular plate-shaped two.
The sheets are arranged in a predetermined set, and iron ions or aluminum ions are eluted into the wastewater storage tank by electrolysis. A power supply supplies a current for electrolysis to each set of electrodes.

【０００９】一組の電極は例えば、両方とも鉄電極及び
アルミニウム電極のうちの１つであり、または一方が鉄
電極及びアルミニウム電極のうちの１つであり他方が不
溶性金属電極である。前者の場合は、所望により電極の
極性反転を行うことで電極の不動態化を防止することが
できる。また、後者の場合は、鉄電極及びアルミニウム
電極のうちの１つをアノードとし、不溶性金属電極をカ
ソードとする。ここで、不溶性金属電極としては、例え
ば銀電極や白金電極などがある。また、一組の電極は例
えば、把手部のある電気絶縁性スペーサなどに固定さ
れ、相互の間隔が一定に保たれているのが好ましい。The set of electrodes is, for example, both one of an iron electrode and an aluminum electrode, or one is one of an iron electrode and an aluminum electrode and the other is an insoluble metal electrode. In the former case, the passivation of the electrode can be prevented by inverting the polarity of the electrode as desired. In the latter case, one of the iron electrode and the aluminum electrode is used as an anode, and the insoluble metal electrode is used as a cathode. Here, examples of the insoluble metal electrode include a silver electrode and a platinum electrode. Further, it is preferable that the pair of electrodes is fixed to, for example, an electrically insulating spacer having a handle, and the interval between the electrodes is kept constant.

【００１０】汚水収納槽に溶出した鉄イオンまたはアル
ミニウムイオンは、汚水中のリン酸（オルトリン酸）と
反応して、水不溶性リン化合物（Ｆｅ（ＯＨ）x （ＰＯ
4 ） y またはＡｌ（ＯＨ）x （ＰＯ4 ）y ）となって凝
集し、汚水収納槽に沈殿する。[0010] Iron ions or aluminum eluted in the sewage storage tank
Minium ions are combined with phosphoric acid (orthophosphoric acid) in wastewater.
React to form a water-insoluble phosphorus compound (Fe (OH)x(PO
Four) yOr Al (OH)x(POFour)y)
Collect and settle in sewage storage tank.

【００１１】制御部は、電極における電流密度を不動態
皮膜の生成が防止できるようにかつ感電のおそれが防止
できるように制御するものである。このように電流密度
を制御するのは、本発明者が研究の結果、不動態化と
電解時の電流密度との間にはなんらかの相関関係がある
こと、電流密度が小さすぎると不動態化が起こるこ
と、電流密度が大きすぎると電極間電圧が上昇して消
費電力が増大するおそれがあること、を突き止めたから
である。The control section controls the current density at the electrode so that the formation of a passive film and the possibility of electric shock can be prevented. As a result of research conducted by the present inventors, there is some correlation between passivation and current density during electrolysis. This is because it has been found that what happens and that if the current density is too high, the voltage between the electrodes increases and power consumption may increase.

【００１２】すなわち、前記鉄イオンを溶出させるよう
な定電流電解を行った場合の適切な電流密度は０．１〜
５．０ｍＡ／ｃｍ2 であり、前記アルミニウムイオンを
溶出させるような定電流電解を行った場合の適切な電流
密度は０．２〜６．０ｍＡ／ｃｍ2 であることが実験か
ら判明した。ここで、電流密度がそれぞれの下限値に満
たないときは不動態化が起こり、それぞれの上限値を越
えたときは電極間電圧が高くなりすぎて消費電力が増大
するおそれがある。なお、消費電力の上限値として電極
間電圧を約２５Ｖに設定した。That is, when a constant current electrolysis for eluting the iron ions is performed, an appropriate current density is 0.1 to 1.0.
Was 5.0 mA / cm 2, that the appropriate current density in the case of performing constant current electrolysis as eluting the aluminum ions is 0.2~6.0mA / cm 2 was found from the experiments. Here, when the current density is less than the respective lower limit, passivation occurs, and when the current density exceeds the respective upper limit, the voltage between electrodes becomes too high and power consumption may increase. In addition, the voltage between electrodes was set to about 25 V as an upper limit of power consumption.

【００１３】これらの電流密度は、前記鉄イオン溶出の
場合、より好ましくは０．２〜４．０ｍＡ／ｃｍ2 、も
っとも好ましくは０．４〜３．０ｍＡ／ｃｍ2 であり、
前記アルミニウムイオン溶出の場合、より好ましくは
０．３〜５．０ｍＡ／ｃｍ2 、もっとも好ましくは０．
６〜４．０ｍＡ／ｃｍ2 であることも判明した。These current densities are more preferably 0.2 to 4.0 mA / cm 2 , most preferably 0.4 to 3.0 mA / cm 2 when the iron ions are eluted,
In the case of the aluminum ion elution, more preferably 0.3 to 5.0 mA / cm 2 , most preferably 0.1 to 5.0 mA / cm 2 .
It was also found to be 6 to 4.0 mA / cm 2 .

【００１４】本発明に係る汚水処理装置は、汚水収納槽
へ流入した汚水が流出後に循環して再び流入するように
構成されている汚水処理装置において、汚水収納槽へ流
入する一日当たりの汚水量をＶ（リットル／日）、汚水
収納槽へ流入する汚水中のリンの濃度をｐ（ｍｇ／リッ
トル）、汚水収納槽へ流入した汚水が流出後に再び流入
するまでの循環時間をＨ（ｓｅｃ）、定数をαとする
と、電極を汚水収納槽の汚水中へ浸漬配置する際の電極
浸漬総表面積Ｓ（ｃｍ2 ）がＳ＝α×ｐ×Ｖ÷Ｈから求
められているのが好ましい。電解中の電極における電流
密度は電流値と電極浸漬総表面積Ｓとから決まるため、
計算により求めた電極浸漬総表面積Ｓに基づいて電極を
汚水収納槽の汚水中へ浸漬配置することで、所望の電流
密度を得ることができるからである。The sewage treatment apparatus according to the present invention is a sewage treatment apparatus in which sewage flowing into a sewage storage tank is circulated after flowing out, and flows in again. Is V (liter / day), the concentration of phosphorus in the sewage flowing into the sewage storage tank is p (mg / liter), and the circulation time until the sewage flowing into the sewage storage tank flows out after flowing out is H (sec). When the constant is α, it is preferable that the total electrode immersion surface area S (cm 2 ) when the electrode is immersed in the sewage in the sewage storage tank is determined from S = α × p × V ÷ H. Since the current density at the electrode during electrolysis is determined by the current value and the total surface area S of the electrode immersion,
This is because a desired current density can be obtained by immersing the electrode in the sewage of the sewage storage tank based on the electrode immersion total surface area S obtained by calculation.

【００１５】例えば、鉄電極をアノードとし、鉄（Ｆ
ｅ）とリン（Ｐ）のモル比Ｆｅ／Ｐをｂとした場合、電
流の強さＡ（ｍＡ）は Ａ＝（ｐ×１０-3÷３０．９７）×Ｖ×２×（９６５００÷Ｈ）×ｂ ＝６．２３×ｂ×ｐ×Ｖ÷Ｈ ……式１ で表される。ここで、３０．９７はリン（Ｐ）の原子
量、２はＦｅ１モル＝２ｇ当量に由来する数値、９６５
００はファラデー定数である。For example, an iron electrode is used as an anode, and iron (F
e) When the molar ratio Fe / P between phosphorus (P) and b is b, the current intensity A (mA) is A = (p × 10 −3 ÷ 30.97) × V × 2 × (96500 ° H) ) × b = 6.23 × b × p × V ÷ H (1) Here, 30.97 is the atomic weight of phosphorus (P), 2 is a numerical value derived from 1 mol of Fe = 2 g equivalent, 965
00 is a Faraday constant.

【００１６】電流密度をａ（ｍＡ／ｃｍ2 ）とするとＳ
は Ｓ＝Ａ／ａ ……式２ で表される。If the current density is a (mA / cm 2 ), S
Is represented by S = A / a Expression 2.

【００１７】したがって、式１と式２から、 Ｓ＝６．２３×ｂ×ｐ×Ｖ÷Ｈ÷ａ ＝α×ｐ×Ｖ÷Ｈ ……式３ で表される。ここで、αはα＝６．２３×ｂ÷ａであっ
て、ａとｂから決まる定数である。Accordingly, from Equations 1 and 2, S = 6.23 × b × p × V ÷ H ÷ a = α × p × V ÷ H (3) Here, α is 6.23 × b ÷ a, and is a constant determined by a and b.

【００１８】本発明に係る汚水処理装置は、電極が、す
べて鉄電極かまたはすべてアルミニウム電極であり、制
御部がさらに、電源に電極の極性反転を指示する機能を
有するとともに、求められたＳの値に応じて適正時間ご
とに１回の極性反転を指示するように構成されているの
が好ましい。極性反転を行うことで、電極の不動態化を
よりいっそう確実に防止して、電気分解の効率化を図る
ことができるからである。In the sewage treatment apparatus according to the present invention, the electrodes are all iron electrodes or all aluminum electrodes, and the control unit further has a function of instructing the power supply to invert the polarity of the electrodes. It is preferable that the polarity inversion is instructed once every appropriate time according to the value. This is because by performing the polarity inversion, the passivation of the electrode can be more reliably prevented, and the efficiency of the electrolysis can be improved.

【００１９】本発明に係る汚水処理装置は、すべての電
極が、鉄及びアルミニウムのうちの一方から構成され、
制御部が、電源に電極の極性反転を指示する機能を有
し、前記定電流電解を行う際に制御部が３０分〜５日間
ごとに１回の極性反転を指示するように構成されている
のが好ましい。一定時間ごとに電極の極性反転を行うこ
とで、電極の不動態化をよりいっそう確実に防止して、
電気分解の効率化を図ることができるからである。In the sewage treatment apparatus according to the present invention, all the electrodes are made of one of iron and aluminum.
The control unit has a function of instructing the power supply to invert the polarity of the electrodes, and is configured to instruct the polarity inversion once every 30 minutes to 5 days when performing the constant current electrolysis. Is preferred. By inverting the polarity of the electrode at regular intervals, the passivation of the electrode is more reliably prevented,
This is because the efficiency of the electrolysis can be improved.

【００２０】[0020]

【発明の実施の形態】以下、本発明の２つの実施の形態
を図面に基づいて説明する。なお、これらによって本発
明が限定されるものではない。DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Two embodiments of the present invention will be described below with reference to the drawings. The present invention is not limited by these.

【００２１】実施の形態１ 図１に示すように、本発明の１つの実施の形態に係る汚
水処理装置Ｄ1 は、１つの汚水収納槽１と、４組の電極
２・３と、各組の電極２・３に電流を供給するための直
流電源（図示略）と、４個の電極保持体４とを備えてな
る。Embodiment 1 As shown in FIG. 1, a sewage treatment apparatus D 1 according to one embodiment of the present invention includes one sewage storage tank 1, four sets of electrodes 2 and 3, And a DC power supply (not shown) for supplying a current to the electrodes 2 and 3 of this embodiment.

【００２２】図２に示すように、汚水収納槽１は平面形
状がほぼ方形の箱からなり、屎尿廃水や生活廃水などの
処理すべき汚水が収納される。汚水収納槽１の対向側壁
の上部には、汚水流入口１ａ及び汚水流出口１ｂが形成
されている。また、汚水収納槽１の底には、左右方向に
延びる２本の底部位置決め棒５が設けられている。そし
て、これらの底部位置決め棒５の内側には、縦方向に延
びる合計６本の左右位置決め棒６が設けられている。As shown in FIG. 2, the sewage storage tank 1 is formed of a box having a substantially rectangular planar shape, and stores sewage to be treated such as human wastewater or domestic wastewater. A sewage inflow port 1a and a sewage outflow port 1b are formed in the upper part of the opposite side wall of the sewage storage tank 1. Further, two bottom positioning rods 5 extending in the left-right direction are provided at the bottom of the sewage storage tank 1. A total of six left and right positioning rods 6 extending in the vertical direction are provided inside these bottom positioning rods 5.

【００２３】各組の電極２・３はいずれも長方形板状の
鉄製であり、汚水中のリン酸を除去する鉄イオンを電気
分解により溶出させる。図３及び図４に拡大して示すよ
うに、一組の電極２・３は、これらの上端に取り付けら
れた塩化ピニル樹脂製の電気絶縁性スペーサ７により、
それらの間隔が一定に保たれている。スペーサ７には把
手部７ａが設けられている。Each of the electrodes 2 and 3 of each set is made of iron in the form of a rectangular plate, and elutes iron ions for removing phosphoric acid in wastewater by electrolysis. As shown in FIG. 3 and FIG. 4 in an enlarged manner, a pair of electrodes 2 and 3 are connected to each other by an electrically insulating spacer 7 made of pinyl chloride resin attached to their upper ends.
Their spacing is kept constant. The spacer 7 is provided with a handle 7a.

【００２４】電極２・３の上端には接続用端子８が設け
られている。これらの端子８はリード線９を介してコネ
クタ１０に接続されている。コネクタ１０は前記電源に
接続される。なお、一組の電極２・３と、１つのスペー
サ７と、２つの端子８と、２つのリード線９と、１つの
コネクタ１０とからなる集合体を説明の便宜上、電極体
１１と称する。The connection terminals 8 are provided at the upper ends of the electrodes 2 and 3. These terminals 8 are connected to a connector 10 via a lead wire 9. The connector 10 is connected to the power supply. An assembly including one set of electrodes 2 and 3, one spacer 7, two terminals 8, two lead wires 9, and one connector 10 is referred to as an electrode body 11 for convenience of description.

【００２５】図３及び図４に拡大して示すように、電極
保持体４は、平面形状が長方形の箱状のものであり、ポ
リプロピレン樹脂製である。電極保持体４の左右両側壁
は、隣り合う電極保持体４どうしを仕切るための電気絶
縁性仕切板４ａにされている。電極保持体４の前後両端
は、ともに長方形の汚水流入口４ｂ及び汚水流出口４ｃ
にされている。As shown in FIGS. 3 and 4 in an enlarged manner, the electrode holder 4 has a rectangular box shape in plan view and is made of polypropylene resin. The left and right side walls of the electrode holder 4 are electrically insulating partition plates 4a for separating the adjacent electrode holders 4 from each other. Both front and rear ends of the electrode holder 4 are rectangular sewage inlet 4b and sewage outlet 4c.
Has been.

【００２６】また、電極保持体４の上下両面は、周縁部
を残して中央が長方形に切り欠かれて、それぞれ電極着
脱口４ｄ及び曝気口４ｅにされている。さらに、電極保
持体４の左右幅（２つの仕切板４ａの外面どうしの間
隔）は、汚水収納槽１内における、隣り合う２つの左右
位置決め棒６どうしの間隔にほぼ等しくされている。な
お、電極保持体４の上面における２つの円形孔４ｆは、
スペーサ７を電極保持体４の上面にネジ止めするための
ものである。The upper and lower surfaces of the electrode holder 4 are notched in a rectangular shape at the center except for the peripheral edge, and are provided with an electrode attachment / detachment opening 4d and an aeration opening 4e, respectively. Further, the left and right width of the electrode holder 4 (the interval between the outer surfaces of the two partition plates 4 a) is substantially equal to the interval between two adjacent left and right positioning rods 6 in the sewage storage tank 1. The two circular holes 4f on the upper surface of the electrode holder 4 are
The spacer 7 is screwed to the upper surface of the electrode holder 4.

【００２７】このように構成された電極保持体４は、汚
水収納槽１内に取出し可能に配される。すなわち、槽内
に設けられた底部位置決め棒５及び左右位置決め棒６に
より定位置にゆるやかに固定される。The electrode holder 4 configured as described above is disposed in the sewage storage tank 1 so as to be able to be taken out. That is, it is loosely fixed to a fixed position by the bottom positioning rod 5 and the left and right positioning rods 6 provided in the tank.

【００２８】また、電極体１１は、電極保持体４に電極
着脱口４ｄから嵌め込まれてスペーサ７が電極保持体４
にネジ止めされることで、電極保持体４に着脱可能に保
持される。したがって、電極２・３の点検や交換の作業
を簡単かつ短時間に行うことができる。また、一組の電
極２・３及び電極保持体４の２つの仕切板４ａは、互い
に平行になっている。したがって、電極保持体４内の汚
水中のＳＳは各電極２・３の電極面に沿って汚水流入口
４ａから汚水流出口４ｂの方へ滞りなく流れる。The electrode body 11 is fitted into the electrode holder 4 from the electrode opening 4d, and the spacer 7 is
, And is detachably held on the electrode holder 4. Therefore, the inspection and replacement work of the electrodes 2 and 3 can be performed easily and in a short time. The two partition plates 4a of the set of electrodes 2 and 3 and the electrode holder 4 are parallel to each other. Therefore, the SS in the sewage in the electrode holder 4 flows from the sewage inlet 4a to the sewage outlet 4b along the electrode surfaces of the electrodes 2 and 3 without interruption.

【００２９】図１及び図２に示すように、電極保持体４
の底面中央は、左右方向へ延びる凹溝部１ｃにされてい
る。そして、この凹溝部１ｃに１つの曝気管１２が嵌め
られている。As shown in FIGS. 1 and 2, the electrode holder 4
The center of the bottom surface is a groove 1c extending in the left-right direction. One aeration tube 12 is fitted in the concave groove 1c.

【００３０】曝気管１２は、この汚水処理装置Ｄ1 が備
える曝気装置の一部である。すなわち、この曝気装置
は、汚水収納槽１外に設けられた給気用ブロア（図示
略）と、このブロアに接続されて槽内へ延びる給気管
（図示略）と、この給気管に接続されて槽底部に配され
た曝気管１２とを備えてなる。The aeration tube 12 is part of the aeration device provided in the sewage treatment apparatus D 1. That is, the aeration apparatus is provided with an air supply blower (not shown) provided outside the sewage storage tank 1, an air supply pipe (not shown) connected to the blower and extending into the tank, and connected to the air supply pipe. And an aeration tube 12 arranged at the bottom of the tank.

【００３１】電極保持体４の曝気口４ｅを通して曝気管
１２から曝気を行うことにより、電極２・３及び仕切板
４ａの洗浄の効果をいっそう上げることができる。By performing aeration from the aeration tube 12 through the aeration port 4e of the electrode holder 4, the effect of cleaning the electrodes 2.3 and the partition plate 4a can be further enhanced.

【００３２】図５に示すように、この汚水処理装置Ｄ1
は小型合併処理浄化槽１０１に組み込まれている。As shown in FIG. 5, this sewage treatment apparatus D 1
Are incorporated in the small-sized combined treatment septic tank 101.

【００３３】浄化槽１０１の内部は、屎尿廃水と生活廃
水との混合した汚水が流入する流入管１０２の側から、
汚水処理ずみの水を外部へ放流する放流管１０３の側に
かけて、汚水浄化処理の工程順に応じて複数の槽が区画
形成された槽構造にされている。The inside of the septic tank 101 is located at a side of an inflow pipe 102 into which sewage mixed with human wastewater and domestic wastewater flows.
A tank structure is formed in which a plurality of tanks are defined and formed in accordance with the order of the sewage purification process on the side of the discharge pipe 103 for discharging sewage treated water to the outside.

【００３４】１０４は流入管１０２側の最前部に区画形
成された第１嫌気濾床槽である。この第１嫌気濾床槽１
０４では、屎尿廃水や生活廃水の中に混入していて浄化
処理できない夾雑物を沈澱分離させて除去する。Reference numeral 104 denotes a first anaerobic filter tank formed at the forefront of the inflow pipe 102 side. This first anaerobic filter bed tank 1
In step 04, impurities that have been mixed in the human wastewater or domestic wastewater and cannot be purified are removed by sedimentation.

【００３５】第１嫌気濾床槽１０４には嫌気性微生物の
濾床である嫌気濾床１０５が設けられており、嫌気濾床
１０５に微生物を棲息させることで嫌気処理を行うよう
にされている。嫌気濾床１０５は、流入水や逆洗廃水が
一時的に流入した際の水流によって沈澱物が巻き上げら
れて浮遊物質となって次の槽へ流出するのを抑えて、次
の槽の負荷を下げることができる。An anaerobic filter bed 105, which is a filter bed for anaerobic microorganisms, is provided in the first anaerobic filter bed tank 104, and anaerobic treatment is performed by inhabiting the microorganisms in the anaerobic filter bed 105. . The anaerobic filter bed 105 suppresses the load on the next tank by preventing the sediment from being lifted up by the water flow when the inflow water or backwash wastewater temporarily flows in and becoming a suspended substance and flowing out to the next tank. Can be lowered.

【００３６】１０６は第１嫌気濾床槽１０４に隣接して
区画形成された次の第２嫌気濾床槽である。第２嫌気濾
床槽１０６では、嫌気濾床１０７に嫌気性微生物を棲息
させることで嫌気処理を行うようにされている。Reference numeral 106 denotes a next second anaerobic filter bed tank formed adjacent to the first anaerobic filter bed tank 104. In the second anaerobic filter bed tank 106, anaerobic microorganisms are made to inhabit the anaerobic filter bed 107 to perform anaerobic treatment.

【００３７】１０８は第２嫌気濾床槽１０６に隣接して
区画形成された次の生物膜濾過槽である。Reference numeral 108 denotes a next biofilm filter tank formed adjacent to the second anaerobic filter bed tank 106.

【００３８】第１嫌気濾床槽１０４と第２嫌気濾床槽１
０６とは垂直な隔壁１０９で仕切られている。隔壁１０
９の上部には、隔壁１０９を貫通する移流口１１０が開
口形成されている。そして、移流口１１０に移流管１１
１が嵌められている。First anaerobic filter tank 104 and second anaerobic filter tank 1
06 is partitioned by a vertical partition wall 109. Partition wall 10
At the upper part of 9, an advection port 110 penetrating the partition wall 109 is formed. Then, the advection pipe 11 is connected to the advection port 110.
1 is fitted.

【００３９】第２嫌気濾床槽１０６と次の生物膜濾過槽
１０８とは垂直な隔壁１１２で仕切られている。隔壁１
１２の上部には、隔壁１１２を貫通する移流口１１３が
開口形成されている。そして、移流口１１３に移流管１
１４が嵌められている。第１嫌気濾床槽１０４から移流
管１１１を通って第２嫌気濾床槽１０６へ移流してきた
汚水は、嫌気濾床１０７を下降流で通過した後、移流管
１１４を通って次の生物膜濾過槽１０８へ送り込まれ
る。The second anaerobic filter bed tank 106 and the next biofilm filtration tank 108 are separated by a vertical partition 112. Partition wall 1
In the upper part of 12, an advection port 113 penetrating the partition wall 112 is formed. Then, the convection pipe 1 is inserted into the convection port 113.
14 is fitted. The sewage that has been transferred from the first anaerobic filter bed tank 104 to the second anaerobic filter tank 106 through the advection tube 111 passes through the anaerobic filter bed 107 in a downward flow, and then passes through the advection tube 114 to the next biofilm. It is sent to the filtration tank 108.

【００４０】第２嫌気濾床槽１０６に設けられた嫌気濾
床１０７により、ある程度のＳＳが捕捉される。捕捉さ
れたＳＳは、徐々に嫌気分解されて溶解性のものになっ
ていったり、第２嫌気濾床槽１０６の底に汚泥として貯
留されたりする。また、嫌気濾床１０７では有機性の窒
素がアンモニア性の窒素に嫌気分解される。A certain amount of SS is captured by the anaerobic filter bed 107 provided in the second anaerobic filter bed tank 106. The trapped SS is gradually anaerobically decomposed and becomes soluble, or is stored as sludge at the bottom of the second anaerobic filter tank 106. In the anaerobic filter bed 107, organic nitrogen is anaerobically decomposed into ammonia nitrogen.

【００４１】生物膜濾過槽１０８には、好気性微生物の
濾床である好気濾床１１５が設けられており、好気濾床
１１５に好気性微生物を棲息させることで好気処理を行
うようにされている。生物膜濾過槽１０８の底部付近に
は、曝気装置の曝気管１１６が横設状態に配されてい
る。曝気装置は、曝気管１１６から空気を吹き出すこと
で、生物膜濾過槽１０８の好気濾床１１５に棲息する好
気性微生物に酸素を供給する。The biofilm filtration tank 108 is provided with an aerobic filter bed 115 which is a filter bed for aerobic microorganisms. The aerobic filter bed 115 is provided with aerobic microorganisms so that aerobic treatment is performed. Has been. In the vicinity of the bottom of the biofilm filtration tank 108, an aeration tube 116 of an aeration device is disposed in a horizontal state. The aeration apparatus supplies oxygen to the aerobic microorganisms living in the aerobic filter bed 115 of the biofilm filtration tank 108 by blowing out air from the aeration pipe 116.

【００４２】１１７は生物膜濾過槽１０８に隣接して区
画形成された次の処理水槽である。処理水槽１１７で
は、生物膜濾過槽１０８で好気処理され、濾過されて移
流してきた処理水を静置貯蔵する。Reference numeral 117 denotes a next treated water tank formed adjacent to the biofilm filtration tank 108. In the treated water tank 117, the treated water that has undergone aerobic treatment in the biofilm filtration tank 108, and has been filtered and advected, is stored in a stationary state.

【００４３】１１８は処理水槽１１７の上部に区画形成
された消毒槽である。消毒槽１１８は、処理水槽１１７
で処理された後の上澄み水を消毒処理して、放流管１０
３から外部へ排出するようにされている。Reference numeral 118 denotes a disinfecting tank formed above the treated water tank 117. The disinfection tank 118 includes a treatment water tank 117.
The supernatant water after disinfection is disinfected, and discharged
3 to the outside.

【００４４】生物膜濾過槽１０８と次の処理水槽１１７
との間には垂直な隔壁１１９で仕切られている。隔壁１
１９の上部には、隔壁１１９を貫通する移流口１２０が
開口形成されている。そして、移流口１２０に移流管１
２１が嵌められている。第２嫌気濾床槽１０６から移流
管１１４を通って生物膜濾過槽１０８へ移流してきた汚
水は、好気濾床１１５を下降流で通過した後、移流管１
２１を通って次の処理水槽１１７へ送り込まれる。Biofilm filtration tank 108 and next treated water tank 117
Are separated by a vertical partition wall 119. Partition wall 1
At the upper part of 19, an advection port 120 penetrating the partition wall 119 is formed. Then, the convection pipe 1 is inserted into the convection port 120.
21 is fitted. The sewage that has flowed from the second anaerobic filter bed tank 106 to the biofilm filtration tank 108 through the advection tube 114 passes through the aerobic filter bed 115 in a descending flow, and then flows through the advection tube 1.
Through 21, it is sent to the next treated water tank 117.

【００４５】処理水槽１１７の上部から第１嫌気濾床槽
１０４の上部にかけて、処理水中の上澄み水を返送する
ための返送管１２２が配されている。そして、処理水槽
１１７からリフト管１２３により汲み上げられた上澄み
水は、分水計量装置１２４、返送管１２２を経て汚水処
理装置Ｄ1 に送られてリン除去処理に供された後に、第
１嫌気濾床槽１０４へ戻される。A return pipe 122 for returning the supernatant water of the treated water is provided from the upper part of the treated water tank 117 to the upper part of the first anaerobic filter bed tank 104. Then, the supernatant water pumped up by the lift tube 123 from the treatment water tank 117, after being subjected diversion metering device 124, is sent through a return pipe 122 to the sewage treatment apparatuses D 1 to the phosphorus removal process, first anaerobic filtration It is returned to the floor tank 104.

【００４６】図５において、１２５は汚水処理装置Ｄ1
が備えている制御部を、１２６は電源をそれぞれ示して
いる。電源１２６は、汚水収納槽１の内部に配された電
極２・３に電気分解のための電流を供給する。１２７は
汚水収納槽１の外部に設けられた給気用ブロアを示す。
ブロア１２７は、汚水収納槽１の内部の電極２・３及び
仕切板４ａに曝気を施すことでこれらの面を洗浄するた
めの曝気装置の一部である。In FIG. 5, reference numeral 125 denotes a sewage treatment apparatus D 1
Denotes a control unit, and 126 denotes a power supply. The power supply 126 supplies a current for electrolysis to the electrodes 2 and 3 arranged inside the sewage storage tank 1. Reference numeral 127 denotes an air supply blower provided outside the sewage storage tank 1.
The blower 127 is a part of an aeration device for washing the electrodes 2 and 3 and the partition plate 4a in the sewage storage tank 1 by aerating these surfaces.

【００４７】浄化槽１０１に流入する汚水の量を１日１
２００リットルとし、浄化槽１０１内の循環流量は６０
００リットルとする。このとき、汚水収納槽１の内部に
配された電極２・３には電流を約６５０ｍＡ流す（鉄イ
オンの溶出量はモル比Ｆｅ／Ｐ＝１．５〜２．５になる
ように制御すればよい）。各電極体１１の電極間距離は
２５ｍｍとされ、電極間電圧は常にモニターできるよう
にされている。なお、電解の際の汚水収納槽１における
電流密度は、前記の式３から得られたＳに基づいて汚水
収納槽１への電極２・３の浸漬深さを適宜調節すること
で、所望の値に設定することができる。The amount of sewage flowing into the septic tank 101 is reduced by 1
200 liters and the circulation flow rate in the septic tank 101 is 60
Assume 00 liters. At this time, a current of about 650 mA flows through the electrodes 2 and 3 disposed inside the sewage storage tank 1 (the elution amount of iron ions is controlled so that the molar ratio Fe / P becomes 1.5 to 2.5). Just fine). The distance between the electrodes of each electrode body 11 is set to 25 mm, and the voltage between the electrodes can be constantly monitored. The current density in the sewage storage tank 1 during electrolysis can be adjusted to a desired value by appropriately adjusting the immersion depth of the electrodes 2 and 3 in the sewage storage tank 1 based on S obtained from Equation 3 above. Can be set to a value.

【００４８】制御部１２５は、前記鉄イオン溶出のため
に電解する際の電流密度を常に０．１〜５．０ｍＡ／ｃ
ｍ2 に維持して定電流電解を行うように、また３０分間
〜５日間ごとに１回の極性反転を指示するように、制御
する。電流密度が０．１ｍＡ／ｃｍ2 に満たないときは
不動態化が起こり、５．０ｍＡ／ｃｍ2 を越えたときは
電極間電圧が約２５Ｖ以上になり消費電力が増大する。The control unit 125 controls the current density at the time of electrolysis for the elution of iron ions to be always 0.1 to 5.0 mA / c.
Control is performed so as to carry out constant current electrolysis while maintaining the pressure at m 2, and to instruct polarity reversal once every 30 minutes to 5 days. When the current density is less than 0.1 mA / cm 2 occurs passivating, power consumption interelectrode voltage becomes greater than or equal to about 25V is increased when it exceeds the 5.0 mA / cm 2.

【００４９】ここでは、浄化槽１０１の運転開始から３
ヶ月間、制御部１２５により電流密度を常に０．３ｍＡ
／ｃｍ2 に維持して、また１時間ごとに１回の極性反転
をしながら定電流電解が行われた。その結果を図６に示
す。Here, three days after the start of operation of the septic tank 101
The current density is always 0.3 mA by the control unit 125 for one month.
/ Cm 2 and constant current electrolysis was performed while reversing the polarity once every hour. FIG. 6 shows the result.

【００５０】図６によれば、運転開始から３ヶ月目にお
ける電極間電圧は、運転開始時におけるそれよりも若干
増えているが、安定している。このときのリン除去率は
８０〜９０％であり、きわめて良好であった。According to FIG. 6, the voltage between the electrodes at the third month from the start of the operation is slightly higher than that at the start of the operation, but is stable. At this time, the phosphorus removal rate was 80 to 90%, which was very good.

【００５１】なお、比較のために、浄化槽１０１の運転
開始から３ヶ月間、制御部１２５により電流密度を常に
０．０５ｍＡ／ｃｍ2 に維持して、また１時間ごとに１
回の極性反転をしながら定電流電解が行われた。その結
果を図７に示す。For comparison, the current density is always maintained at 0.05 mA / cm 2 by the control unit 125 for three months from the start of operation of the septic tank 101, and the current density is maintained at 1 hour every one hour.
Constant current electrolysis was performed while reversing the polarity several times. FIG. 7 shows the result.

【００５２】図７によれば、運転開始から３ヶ月目にお
ける電極間電圧は運転開始時におけるそれよりも高くな
っている。また、電極２・３のアノード側で酸素ガスの
発生が認められた。これは、アノード側で溶出する前記
鉄イオンの量が低下し、水の電解が起こっていることを
示す。その原因としては、電極２・３の表面にＦｅ3Ｏ
4 などの不動態皮膜が形成されたためであると思われ
る。この場合、鉄イオンの溶出量が低下する分、リン除
去率が低下する。この電流密度でさらに浄化槽１０１の
連続運転を行うと、電極間電圧が上昇して消費電力が増
大する。According to FIG. 7, the voltage between the electrodes in the third month from the start of the operation is higher than that at the start of the operation. Further, generation of oxygen gas was observed on the anode sides of the electrodes 2 and 3. This indicates that the amount of the iron ions eluted on the anode side has decreased, and electrolysis of water has occurred. The reason for this is that Fe 3 O
This is probably because a passive film such as 4 was formed. In this case, as the elution amount of iron ions decreases, the phosphorus removal rate decreases. When the septic tank 101 is further operated at this current density, the voltage between the electrodes increases, and the power consumption increases.

【００５３】なお、電極２・３から溶出した鉄イオン
は、汚水中に含まれるリン酸イオンと凝集反応してリン
酸鉄塩や水酸化鉄を生成する。この反応はアノード側で
起こると考えられる。カソード側では水素ガスが発生す
る。この水素ガスは、電極２・３の表面への不動態皮膜
や有機性付着物の生成を防止したり除去したりする効果
を有している。つまり、この水素ガス自身が電極２・３
の洗浄効果をもたらす。電流密度が小さすぎる場合、こ
の水素ガスの発生量が少なくなる分、不動態皮膜の生成
が進行する。The iron ions eluted from the electrodes 2 and 3 undergo an aggregation reaction with the phosphate ions contained in the sewage to produce iron phosphate and iron hydroxide. This reaction is believed to take place on the anode side. Hydrogen gas is generated on the cathode side. The hydrogen gas has an effect of preventing or removing the formation of a passivation film and organic deposits on the surfaces of the electrodes 2 and 3. That is, the hydrogen gas itself is used as the electrodes 2 and 3
Brings a cleaning effect. If the current density is too low, the generation of the passive film proceeds as much as the amount of generated hydrogen gas decreases.

【００５４】次に、電流密度を常に０．３〜５．０ｍＡ
／ｃｍ2 の範囲内における種々の一定値に維持し、また
３０分間〜５日間ごとに１回の極性反転をして定電流電
解を行った。それらの結果はいずれも、安定したリン除
去効果の認められるものであった。Next, the current density is always set to 0.3 to 5.0 mA.
/ Cm 2 , and a constant current electrolysis was carried out by inverting the polarity once every 30 minutes to 5 days. All of these results showed a stable phosphorus removal effect.

【００５５】この汚水処理装置Ｄ1 における汚水収納槽
１の汚水中へ電極２・３を浸漬配置する際の電極浸漬総
表面積Ｓ（ｃｍ2 ）は、所望の電流密度を得るために、
前記の式３から求められている。The electrode immersion total surface area S (cm 2 ) when the electrodes 2 and 3 are immersed and disposed in the sewage of the sewage storage tank 1 in the sewage treatment apparatus D 1 is determined in order to obtain a desired current density.
It is determined from Equation 3 above.

【００５６】例えば、流入側のリン濃度ｐを５ｍｇ／リ
ットルとしたとき、モル比Ｆｅ／Ｐ１．０〜２．５の範
囲（この範囲が適切であり、さらに１．５〜２．０が有
効である）のうち、１．５を利用すれば、必要な鉄濃度
は１４ｍｇ／リットルとなる。汚水処理装置Ｄ1 への汚
水の流入量及び循環時間をそれぞれ１２００リットル／
日、２３．５時間とすると、汚水収納槽１における電解
電流値は６９０ｍＡとなる。For example, when the phosphorus concentration p on the inflow side is 5 mg / liter, the molar ratio Fe / P is in the range of 1.0 to 2.5 (this range is appropriate, and 1.5 to 2.0 is more effective). If 1.5 is used, the required iron concentration is 14 mg / liter. Inflow wastewater to the sewage treatment apparatus D 1 and circulation time of each 1200 l /
Assuming 23.5 hours per day, the electrolytic current value in the sewage storage tank 1 is 690 mA.

【００５７】したがって、所望の電流密度ａを１．０ｍ
Ａ／ｃｍ2 に設定すると、式３からＳは６９０ｃｍ2 に
決められる。Therefore, the desired current density a is set to 1.0 m
When set to A / cm 2, from Equation 3 S is determined in 690 cm 2.

【００５８】つまり、流入リン濃度、汚水流入量、循環
時間が決まれば、最適な電極浸漬総表面積を求めること
が可能になる。That is, if the concentration of the inflowing phosphorus, the amount of inflowing sewage, and the circulation time are determined, it is possible to obtain the optimum total surface area of the electrode immersion.

【００５９】実施の形態２ 図８に示すように、本発明の他の１つの実施の形態に係
る汚水処理装置Ｄ2 は、１つの汚水収納槽１と、４組の
鉄製電極と、各組の電極に電流を供給するための直流電
源１２６と、給気用ブロア１２７と、視覚的報知部であ
るＬＥＤランプ１２８と、制御部１２９とを備えてな
る。Embodiment 2 As shown in FIG. 8, a sewage treatment apparatus D 2 according to another embodiment of the present invention includes one sewage storage tank 1, four sets of iron electrodes, A DC power supply 126 for supplying current to the electrodes, an air supply blower 127, an LED lamp 128 as a visual notification unit, and a control unit 129.

【００６０】電極は汚水処理装置Ｄ1 におけるものと同
じである。ＬＥＤランプ１２８は、電解中の電極間電圧
が２５Ｖ以上になると点灯することで、それを外部へ視
覚的に報知する。この点灯は制御部１２９の指示により
行われる。[0060] electrode is the same as in sewage treatment apparatus D 1. The LED lamp 128 is turned on when the voltage between the electrodes during electrolysis becomes 25 V or more, thereby visually notifying the outside to the outside. This lighting is performed according to an instruction from the control unit 129.

【００６１】制御部１２９は、電流密度が０．１ｍＡ／
ｃｍ2 を下回る定電流電解を行う場合には、電流密度を
定期的かつ一時的に０．１〜５．０ｍＡ／ｃｍ2 に上昇
させるように制御する。その１例を図９に示す。The control unit 129 determines that the current density is 0.1 mA /
When performing constant current electrolysis below cm 2 , control is performed so that the current density is periodically and temporarily increased to 0.1 to 5.0 mA / cm 2 . One example is shown in FIG.

【００６２】すなわち、図９の上側に示すように、電流
密度を０．０５ｍＡ／ｃｍ2 に維持して１２時間ごとに
１回の極性反転をして定電流電解を行った場合には、リ
ン除去効果が悪かった。これは電極表面に不動態皮膜の
生成が起きたためと思われる。図９の下側に示すよう
に、０．０５ｍＡ／ｃｍ2 の電流密度で１０時間の定電
流電解を行い、次いで０．２ｍＡ／ｃｍ2 の電流密度で
２時間の定電流電解を行い、その後に極性反転をして、
再び０．０５ｍＡ／ｃｍ2 の電流密度で１０時間の定電
流電解を行った場合には、高いリン除去効果が認められ
た。これは、生成した不動態皮膜が電流密度の一時的上
昇によって破壊除去されたためと考えられる。That is, as shown in the upper part of FIG. 9, when the current density is maintained at 0.05 mA / cm 2 and the polarity is inverted once every 12 hours to carry out constant current electrolysis, The removal effect was poor. This is presumably because a passivation film was formed on the electrode surface. As shown in the lower part of FIG. 9, 0.05 mA / cm was treated with constant current electrolysis for 10 hours in 2 current density, then subjected to constant current electrolysis in 2 hours at a current density of 0.2 mA / cm 2, then With polarity reversal,
When constant current electrolysis was performed again at a current density of 0.05 mA / cm 2 for 10 hours, a high phosphorus removing effect was observed. This is considered to be because the generated passive film was destroyed and removed due to a temporary increase in current density.

【００６３】このような高いリン除去効果は、電流密度
を一時的に上昇させることにより維持することができ
る。Such a high phosphorus removal effect can be maintained by temporarily increasing the current density.

【００６４】汚水処理装置Ｄ2 の他の部分の構成及び汚
水処理装置Ｄ2 が奏する効果は、汚水処理装置Ｄ1 のそ
れと実質的に同様であるので、詳細な説明は省略する。[0064] Sewage treatment apparatus other part effects configuration and sewage treatment device D 2 exhibit of D 2 are the same substantially similar sewage treatment apparatus D 1, detailed description thereof will be omitted.

【００６５】[0065]

【発明の効果】請求項１記載の発明によれば、汚水収納
槽と、汚水中のリン酸を除去するための鉄イオンまたは
アルミニウムイオンを電気分解により溶出させるための
電極と、電極に電解用電流を供給するための電源と、制
御部とを備えてなり、制御部が、電極における電流密度
を不動態皮膜の溶出の生成が防止できるようにかつ電極
間電圧の上昇が防止できるように制御する。したがっ
て、電流密度を適切な値に維持して定電流電解を行うこ
とで、汚水中に不溶性リン酸塩形成金属イオンを電気化
学的に溶出させる際の不動態化を防止して、汚水中のリ
ン酸を安定的に除去するとともに、消費電力の増大を防
止することができる。According to the first aspect of the present invention, a sewage storage tank, an electrode for eluting iron ions or aluminum ions for removing phosphoric acid in sewage by electrolysis, and an electrode for electrolysis are provided. A power supply for supplying a current, and a control unit, wherein the control unit controls the current density at the electrodes so as to prevent generation of elution of the passive film and to prevent an increase in inter-electrode voltage. I do. Therefore, by performing constant current electrolysis while maintaining the current density at an appropriate value, it is possible to prevent passivation when electrochemically eluting insoluble phosphate-forming metal ions into the wastewater, and to prevent Phosphoric acid can be stably removed, and an increase in power consumption can be prevented.

【００６６】請求項２記載の発明によれば、制御部が、
前記電流密度を、鉄イオン溶出のときは０．１〜５．０
ｍＡ／ｃｍ2 の範囲内の一定値に、アルミニウムイオン
溶出のときは０．２〜６．０ｍＡ／ｃｍ2 の範囲内の一
定値に維持して定電流電解を行うように制御する。した
がって、電極間電圧の異常上昇を防止し電流密度を適切
な値に維持することで、請求項１記載の発明に係る前記
効果をいっそう確実に奏することができる。According to the second aspect of the present invention, the control unit includes:
The current density is 0.1 to 5.0 when iron ions are eluted.
to a constant value in the range of mA / cm 2, when the aluminum ion elution is controlled so as to perform constant current electrolysis was maintained at a constant value in the range of 0.2~6.0mA / cm 2. Therefore, by preventing the abnormal increase in the voltage between the electrodes and maintaining the current density at an appropriate value, the effect according to the first aspect of the present invention can be more reliably achieved.

【００６７】請求項３記載の発明によれば、汚水収納槽
へ流入した汚水が流出後に循環して再び流入するように
構成されている汚水処理装置において、汚水収納槽へ流
入する一日当たりの汚水量をＶ（リットル／日）、汚水
収納槽へ流入する汚水中のリンの濃度をｐ（ｍｇ／リッ
トル）、汚水収納槽へ流入した汚水が流出後に再び流入
するまでの循環時間をＨ（ｓｅｃ）、定数をαとする
と、電極を汚水収納槽の汚水中へ浸漬配置する際の電極
浸漬総表面積Ｓ（ｃｍ2 ）がＳ＝α×ｐ×Ｖ÷Ｈから求
められている。したがって、電解中の電極における電流
密度は電流値と電極浸漬総表面積Ｓとから決まるため、
計算により求めた電極浸漬総表面積Ｓに基づいて電極を
汚水収納槽の汚水中へ浸漬配置することで、所望の電流
密度を得ることができる。According to the third aspect of the present invention, in a sewage treatment apparatus configured so that sewage flowing into a sewage storage tank is circulated after flowing out and re-entered, sewage per day flowing into the sewage storage tank is provided. The amount is V (liter / day), the concentration of phosphorus in the sewage flowing into the sewage storage tank is p (mg / liter), and the circulation time until the sewage flowing into the sewage storage tank flows out after flowing out is H (sec). ), Where α is a constant, the total electrode immersion surface area S (cm 2 ) when the electrode is immersed in the sewage of the sewage storage tank is determined from S = α × p × V ÷ H. Therefore, since the current density at the electrode during electrolysis is determined by the current value and the total surface area S of the electrode immersion,
The desired current density can be obtained by immersing the electrodes in the sewage of the sewage storage tank based on the electrode immersion total surface area S obtained by calculation.

【００６８】請求項４記載の発明によれば、電極が、す
べて鉄電極かまたはすべてアルミニウム電極であり、制
御部がさらに、電源に電極の極性反転を指示する機能を
有するとともに、求められたＳの値に応じて適正時間ご
とに１回の極性反転を指示する。したがって、一定時間
ごとに電極の極性反転を行うことで、請求項３記載の発
明が奏する電極の不動態化をよりいっそう確実に防止し
て、電気分解の効率化を図ることができる。According to the fourth aspect of the present invention, the electrodes are all iron electrodes or all aluminum electrodes, and the control unit further has a function of instructing the power supply to invert the polarity of the electrodes. Is instructed once every appropriate time according to the value of. Therefore, by inverting the polarity of the electrode at regular intervals, the passivation of the electrode according to the invention of claim 3 can be more reliably prevented, and the efficiency of electrolysis can be improved.

【図面の簡単な説明】[Brief description of the drawings]

【図１】本発明の実施の形態１に係る汚水処理装置の分
解斜視図である。FIG. 1 is an exploded perspective view of a sewage treatment apparatus according to Embodiment 1 of the present invention.

【図２】図１の汚水処理装置の一部を上面から見た構成
説明図である。FIG. 2 is a configuration explanatory view of a part of the sewage treatment apparatus of FIG. 1 as viewed from above.

【図３】図１の汚水処理装置の構成部材である電極体及
び電極保持体の斜視図である。FIG. 3 is a perspective view of an electrode body and an electrode holder which are components of the sewage treatment apparatus of FIG.

【図４】図３の電極体及び電極保持体の分解斜視図であ
る。FIG. 4 is an exploded perspective view of the electrode body and the electrode holder of FIG.

【図５】図１の汚水処理装置が組み込まれた合併処理浄
化槽の内部を正面から見た拡大構成説明図である。FIG. 5 is an enlarged configuration explanatory view of the inside of the merged treatment septic tank incorporating the sewage treatment apparatus of FIG. 1 as viewed from the front.

【図６】図１の汚水処理装置により電流密度を常に０．
３ｍＡ／ｃｍ2 に維持して、また１時間ごとに１回の極
性反転をしながら定電流電解を行ったときの電極間電圧
の変化を示すグラフである。FIG. 6: The current density is always set to 0 by the sewage treatment apparatus of FIG.
It is a graph which shows the change of the voltage between electrodes when constant current electrolysis is performed, maintaining 3 mA / cm < 2 > and inverting the polarity once every hour.

【図７】図１の汚水処理装置により電流密度を常に０．
０５ｍＡ／ｃｍ2 に維持して、また１時間ごとに１回の
極性反転をしながら定電流電解を行ったときの電極間電
圧の変化を示すグラフである。FIG. 7: The current density is always set to 0 by the sewage treatment apparatus of FIG.
It is a graph which shows the change of the voltage between electrodes when performing constant current electrolysis while maintaining it at 05 mA / cm < 2 > and inverting the polarity once every hour.

【図８】本発明の実施の形態２に係る汚水処理装置が組
み込まれた合併処理浄化槽の内部を正面から見た拡大構
成説明図である。FIG. 8 is an enlarged configuration explanatory view of the inside of a merged treatment septic tank in which a sewage treatment apparatus according to Embodiment 2 of the present invention is incorporated, as viewed from the front.

【図９】図８の汚水処理装置により電流密度が０．１ｍ
Ａ／ｃｍ2 を下回る定電流電解を行ったときの電極間電
圧の変化と、電流密度を定期的かつ一時的に０．１〜
５．０ｍＡ／ｃｍ2 に上昇させたときの電極間電圧の変
化とを示すグラフである。9 shows a current density of 0.1 m by the sewage treatment apparatus of FIG.
A change in interelectrode voltage when a constant current electrolysis of less than A / cm 2 is performed, and a current density of 0.1 to 0.1
It is a graph which shows the change of the voltage between electrodes at the time of raising to 5.0 mA / cm < 2 >.

【符号の説明】[Explanation of symbols]

１ 汚水収納槽 ２ 電極 ３ 電極 Ｄ1 汚水処理装置 Ｄ2 汚水処理装置 １０１ 小型合併処理浄化槽 １２５ 制御部 １２６ 電源 １２９ 制御部Reference Signs List 1 sewage storage tank 2 electrode 3 electrode D 1 sewage treatment device D 2 sewage treatment device 101 small combined treatment / purification tank 125 control unit 126 power supply 129 control unit

───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.6 識別記号 ＦＩ Ｃ０２Ｆ 3/12 ──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. 6 Identification code FI C02F 3/12

Claims (4)

【特許請求の範囲】[Claims] 【請求項１】 汚水収納槽と、この汚水収納槽に配さ
れ、その汚水中のリン酸を沈殿除去するための鉄イオン
またはアルミニウムイオンを電気分解により溶出する少
なくとも一組の電極と、この電極に電解用電流を供給す
るための電源と、電極における電流密度を不動態皮膜の
生成が防止できるようにかつ電極間電圧の上昇が防止で
きるように制御する制御部とを備えてなることを特徴と
する汚水処理装置。1. A sewage storage tank, at least one set of electrodes disposed in the sewage storage tank and eluting iron ions or aluminum ions for precipitating and removing phosphoric acid in the sewage by electrolysis, and the electrodes A power supply for supplying a current for electrolysis to the electrode, and a control unit for controlling the current density at the electrodes so as to prevent generation of a passivation film and to prevent a rise in inter-electrode voltage. Wastewater treatment equipment. 【請求項２】 制御部が、前記電流密度を、鉄イオン溶
出のときは０．１〜５．０ｍＡ／ｃｍ2 の範囲内の一定
値に、アルミニウムイオン溶出のときは０．２〜６．０
ｍＡ／ｃｍ2 の範囲内の一定値に維持して定電流電解を
行うように制御する請求項１記載の汚水処理装置。2. The control section sets the current density to a constant value in the range of 0.1 to 5.0 mA / cm 2 when iron ions are eluted, and 0.2 to 6.5 when aluminum ions are eluted. 0
2. The sewage treatment apparatus according to claim 1, wherein the sewage treatment apparatus is controlled to perform constant current electrolysis while maintaining a constant value within a range of mA / cm < 2 >. 【請求項３】 汚水収納槽へ流入した汚水が流出後に循
環して再び流入するように構成されている汚水処理装置
において、汚水収納槽へ流入する一日当たりの汚水量を
Ｖ（リットル／日）、汚水収納槽へ流入する汚水中のリ
ンの濃度をｐ（ｍｇ／リットル）、汚水収納槽へ流入し
た汚水が流出後に再び流入するまでの循環時間をＨ（ｓ
ｅｃ）、定数をαとすると、電極を汚水収納槽の汚水中
へ浸漬配置する際の電極浸漬総表面積Ｓ（ｃｍ2 ）がＳ
＝α×ｐ×Ｖ÷Ｈから求められている請求項１または２
記載の汚水処理装置。3. A sewage treatment apparatus in which sewage flowing into a sewage storage tank is configured to circulate after flowing out and flow again, and the amount of sewage flowing into the sewage storage tank per day is V (liter / day). The concentration of phosphorus in the sewage flowing into the sewage storage tank is p (mg / liter), and the circulation time until the sewage flowing into the sewage storage tank flows out after flowing out is H (s).
ec), assuming that the constant is α, the electrode immersion total surface area S (cm 2 ) when the electrode is immersed in the sewage in the sewage storage tank is S
= Α × p × V ÷ H.
A sewage treatment apparatus according to claim 1. 【請求項４】 電極が、すべて鉄電極かまたはすべてア
ルミニウム電極であり、制御部がさらに、電源に電極の
極性反転を指示する機能を有するとともに、求められた
Ｓの値に応じて適正時間ごとに１回の極性反転を指示す
る請求項３記載の汚水処理装置。4. The electrodes are all iron electrodes or all aluminum electrodes, and the control unit further has a function of instructing the power supply to invert the polarity of the electrodes, and at appropriate time intervals according to the obtained value of S. 4. The sewage treatment apparatus according to claim 3, wherein a single polarity inversion is instructed.
JP35879797A 1997-12-26 1997-12-26 Sewage treatment equipment Expired - Lifetime JP3796033B2 (en)

Priority Applications (4)

Application Number Priority Date Filing Date Title
JP35879797A JP3796033B2 (en) 1997-12-26 1997-12-26 Sewage treatment equipment
TW087119085A TW442444B (en) 1997-12-26 1998-11-18 Sewage treatment apparatus
KR1019980055179A KR100293311B1 (en) 1997-12-26 1998-12-15 Sewage Treatment Equipment
CN98125540A CN1220975A (en) 1997-12-26 1998-12-21 Sewage treatment device

Applications Claiming Priority (1)

Application Number Priority Date Filing Date Title
JP35879797A JP3796033B2 (en) 1997-12-26 1997-12-26 Sewage treatment equipment

Publications (2)

Publication Number Publication Date
JPH11188365A true JPH11188365A (en) 1999-07-13
JP3796033B2 JP3796033B2 (en) 2006-07-12

Family

ID=18461166

Family Applications (1)

Application Number Title Priority Date Filing Date
JP35879797A Expired - Lifetime JP3796033B2 (en) 1997-12-26 1997-12-26 Sewage treatment equipment

Country Status (4)

Country Link
JP (1) JP3796033B2 (en)
KR (1) KR100293311B1 (en)
CN (1) CN1220975A (en)
TW (1) TW442444B (en)

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002045859A (en) * 2000-07-31 2002-02-12 Sanyo Electric Co Ltd Sewage treating device and method for detecting time for exchanging ion supply electrode pair
CN103583417A (en) * 2012-08-14 2014-02-19 虞文豪 Aquaculture sterilizing device and application thereof
TWI463944B (en) * 2012-08-14 2014-12-11 Yu Wen Hao Sterilization device for aquaculture and its application

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN102964038A (en) * 2012-12-20 2013-03-13 山东国辰环境科技有限公司 Integrated unattended reclaimed water treatment plant

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2002045859A (en) * 2000-07-31 2002-02-12 Sanyo Electric Co Ltd Sewage treating device and method for detecting time for exchanging ion supply electrode pair
CN103583417A (en) * 2012-08-14 2014-02-19 虞文豪 Aquaculture sterilizing device and application thereof
TWI463944B (en) * 2012-08-14 2014-12-11 Yu Wen Hao Sterilization device for aquaculture and its application

Also Published As

Publication number Publication date
KR100293311B1 (en) 2001-07-12
TW442444B (en) 2001-06-23
JP3796033B2 (en) 2006-07-12
CN1220975A (en) 1999-06-30
KR19990063079A (en) 1999-07-26

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