JP2002018443A - Method and apparatus for water treatment - Google Patents
Method and apparatus for water treatmentInfo
- Publication number
- JP2002018443A JP2002018443A JP2000208643A JP2000208643A JP2002018443A JP 2002018443 A JP2002018443 A JP 2002018443A JP 2000208643 A JP2000208643 A JP 2000208643A JP 2000208643 A JP2000208643 A JP 2000208643A JP 2002018443 A JP2002018443 A JP 2002018443A
- Authority
- JP
- Japan
- Prior art keywords
- water
- electrolytic cell
- treated
- supplied
- water treatment
- 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.)
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Links
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Landscapes
- Activated Sludge Processes (AREA)
- Treatment Of Water By Oxidation Or Reduction (AREA)
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、汚染物質を含有す
る被処理水を、電気分解を利用して処理する水処理方法
及び水処理装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a water treatment method and a water treatment apparatus for treating treated water containing pollutants by using electrolysis.
【０００２】[0002]
【従来の技術】近年、上水、下水、屎尿、ごみの埋め立
て浸出水や各種産業廃水等においてダイオキシン類、環
境ホルモン物質、その他の有害有機化合物等の汚染物質
による汚染が問題になっており、これら汚染物質の処理
方法が切望されている。2. Description of the Related Art In recent years, pollutants such as dioxins, environmental hormones, and other harmful organic compounds have become a problem in clean water, sewage, human waste, leachate leachate, and various industrial wastewaters. There is a long-felt need for a method for treating these contaminants.
【０００３】これら汚染物質の処理方法としては、例え
ば、活性炭等の吸着剤を利用する吸着法、光触媒として
のＴｉＯ2と紫外線を使用する光触媒法や、オゾン等の
酸化剤と紫外線を併用する促進酸化法等が知られてい
る。[0003] As a method of treating these contaminants, for example, an adsorption method using an adsorbent such as activated carbon, a photocatalyst method using TiO 2 as a photocatalyst and ultraviolet light, and an acceleration method using an oxidant such as ozone and ultraviolet light together are used. Oxidation methods and the like are known.
【０００４】上記吸着法では、使用に連れ性能が低下す
るため、吸着剤を再生炉で再生した後、再充填しなけれ
ばならないという問題があり、光触媒法や促進酸化法で
は、紫外線照射設備が必要であるといった問題に加え
て、光を反応器の内部まで導光するための工夫が必要で
あり、さらに光を照射するランプの劣化問題もある。[0004] In the above-mentioned adsorption method, the performance deteriorates with use. Therefore, there is a problem that the adsorbent must be refilled after being regenerated in a regeneration furnace. In the photocatalytic method and the accelerated oxidation method, ultraviolet irradiation equipment is required. In addition to the problem of necessity, it is necessary to devise a way to guide light to the inside of the reactor, and there is also a problem of deterioration of the lamp that irradiates light.
【０００５】これらの方法以外の比較的簡易な処理方法
として、汚染物質を含有する被処理水を、板状或いは棒
状等の陽極と陰極を交互に配置した電解槽に供給し、電
気分解で処理する電解法が知られている。As a relatively simple treatment method other than these methods, water to be treated containing contaminants is supplied to an electrolytic cell having a plate-like or rod-like shape in which anodes and cathodes are alternately arranged, and treated by electrolysis. A known electrolysis method is known.
【０００６】[0006]
【発明が解決しようとする課題】この電解処理では、電
解により陰極近傍がアルカリ性に、陽極近傍が酸性に各
々なるため、被処理水中にＣａ2+、Ｍｇ2+、炭酸イオン
が存在すると、陰極表面に炭酸カルシウム、炭酸マグネ
シウムが析出する。ここで、純水等の特殊な水を除く
と、通常の廃水には必ずカルシウム、マグネシウム、炭
酸が存在するため、電極に対する炭酸カルシウムや炭酸
マグネシウムの析出、付着の問題は必然的に生じること
になる。また、陽極に酸化被膜が生成したり、両極にオ
イルやその他の汚染物質が付着することもある。In this electrolytic treatment, since the vicinity of the cathode becomes alkaline and the vicinity of the anode becomes acidic due to electrolysis, if Ca 2+ , Mg 2+ and carbonate ions are present in the water to be treated, the cathode will Calcium carbonate and magnesium carbonate precipitate on the surface. Here, except for special water such as pure water, ordinary wastewater always contains calcium, magnesium, and carbonic acid, so that the problem of precipitation and adhesion of calcium carbonate and magnesium carbonate to the electrodes necessarily occurs. Become. Also, an oxide film may be formed on the anode, and oil and other contaminants may adhere to both electrodes.
【０００７】これらは非導電性のため、電解槽に流す電
流が低下して電解効率が低下し、これらの堆積物が経時
的に多くなると、電解が不可能となるという不具合が生
じる。[0007] Since these are non-conductive, the current flowing through the electrolytic cell is reduced to lower the electrolysis efficiency, and if these deposits increase with time, electrolysis becomes impossible.
【０００８】このような場合、電極を取り出して洗浄す
るか、電解槽に薬剤を充満させて洗浄しなければなら
ず、大変な労力を必要とする。また、薬剤を使用した場
合には、薬剤の処理が必要となる。また、電極を洗浄す
る他の方法として、定期的に電極表面を摺動するクリー
ナを設置することも考えられるが、厄介な設備となる。
また、他の洗浄方法として、定期的に陽極と陰極を切り
換える簡単な方法が知られているが、一度析出した炭酸
カルシウムや炭酸マグネシウムを除去するのは難しい。
また、この方法では、廃水中の油や固形物が付着した電
極の汚れに対する効果は期待できない。In such a case, the electrode must be taken out and washed, or the electrolytic cell must be filled with a chemical and washed, which requires a great deal of labor. Further, when a medicine is used, the treatment of the medicine is required. As another method of cleaning the electrode, it is conceivable to periodically install a cleaner that slides on the surface of the electrode, but this is troublesome equipment.
As another cleaning method, a simple method of periodically switching between an anode and a cathode is known, but it is difficult to remove calcium carbonate and magnesium carbonate once deposited.
In addition, this method cannot be expected to have any effect on the contamination of the electrode to which the oil or solid matter in the wastewater has adhered.
【０００９】そこで、例えば特開平１１−２９０８５７
号公報には、電極の下部から散気する気泡により電極を
清掃する方法が、また、例えば実開平６−６０４９９号
公報には、散気に加えて電解槽に撹拌翼を設置して電極
表面を洗浄する方法が、比較的簡易な方法として各々提
案されている。Therefore, for example, Japanese Patent Application Laid-Open No. H11-290857
Japanese Patent Application Laid-Open No. 6-60499 discloses a method of cleaning an electrode by using bubbles scattered from the lower part of the electrode. Have been proposed as relatively simple methods.
【００１０】しかしながら、これらの方法では、ある程
度の改善は可能であるが、単なる水流による洗浄である
ため、その効果は十分とはいえない。[0010] However, these methods can be improved to some extent, but their effects are not sufficient because they are merely washing with water flow.
【００１１】本発明は、このような課題を解決するため
になされたものであり、電解槽の電極を十分に洗浄し、
電気分解を経時的に安定して行い得る水処理方法及び水
処理装置を提供することを目的とする。The present invention has been made in order to solve such a problem, and has been made to sufficiently wash an electrode of an electrolytic cell,
An object of the present invention is to provide a water treatment method and a water treatment apparatus capable of performing electrolysis stably over time.
【００１２】[0012]
【課題を解決するための手段】本発明による水処理方法
は、陽極と陰極を備える電解槽に、汚染物質を含有する
被処理水を供給し、電解槽に供給された浮遊固体と共に
被処理水を流動化させて当該被処理水を電解処理するこ
とを特徴としている。According to the water treatment method of the present invention, the water to be treated containing contaminants is supplied to an electrolytic cell having an anode and a cathode, and the water to be treated is treated together with the suspended solid supplied to the electrolytic cell. Is fluidized and the water to be treated is subjected to electrolytic treatment.
【００１３】このような水処理方法によれば、流動化さ
れる浮遊固体が電極に衝突するため、当該電極の付着物
が効果的に剥離される。According to such a water treatment method, since the floating solid to be fluidized collides with the electrode, the deposits on the electrode are effectively peeled off.
【００１４】ここで、浮遊固体を、被処理水の供給前に
予め電解槽に供給していても、被処理水の供給後に電解
槽に供給するようにしても良い。Here, the suspended solid may be supplied to the electrolytic cell in advance before supplying the water to be treated, or may be supplied to the electrolytic cell after supplying the water to be treated.
【００１５】特に、電極の汚れの度合いを検出し、当該
電極が所定に汚れたら、浮遊固体を電解槽に供給するよ
うにすれば、陽極からの金属の溶出を防止すべく当該陽
極に例えば白金等の鍍金を施している場合には、この鍍
金に対する浮遊固体の衝突の機会が必要最低限とされ、
当該鍍金の剥離の虞が低減される。In particular, if the degree of contamination of the electrode is detected, and if the electrode is contaminated to a predetermined degree, a suspended solid is supplied to the electrolytic cell, and for example, platinum is applied to the anode to prevent elution of metal from the anode. In the case of plating, etc., the chance of collision of suspended solids with this plating is minimized,
The possibility of peeling of the plating is reduced.
【００１６】また、電解槽にガスを供給して、被処理水
及び浮遊固体を流動化させるのが好ましい。It is preferable to supply gas to the electrolytic cell to fluidize the water to be treated and the suspended solids.
【００１７】このように、被処理水及び浮遊固体の流動
化を、撹拌翼等の機械的手段ではなくガス供給で行うこ
とで、電解槽の簡素化が図られる。As described above, the fluidization of the water to be treated and the suspended solids is performed not by mechanical means such as stirring blades but by gas supply, thereby simplifying the electrolytic cell.
【００１８】また、ガスを酸素含有ガスとし、電解槽に
生物汚泥を共存させて被処理水を電解処理しても良い。Further, the gas to be treated may be an oxygen-containing gas, and the water to be treated may be subjected to electrolytic treatment in the presence of biological sludge in the electrolytic cell.
【００１９】このように、電解槽に生物汚泥を共存させ
ることで、有機物を分解する生物汚泥槽としての機能も
有することになる。また、被処理水及び浮遊固体を流動
化させるガスを、酸素含有ガスとすれば、生物汚泥に必
要な酸素含有ガスを別途供給の必要がない。As described above, by coexisting biological sludge in the electrolytic cell, it also has a function as a biological sludge tank for decomposing organic substances. Further, if the gas for fluidizing the water to be treated and the suspended solids is an oxygen-containing gas, there is no need to separately supply an oxygen-containing gas necessary for biological sludge.
【００２０】また、電解槽に、過酸化水素及びオゾンの
少なくとも一方を供給して被処理水を電解処理するのが
好ましい。Preferably, at least one of hydrogen peroxide and ozone is supplied to the electrolysis tank to electrolyze the water to be treated.
【００２１】このような構成を採用した場合、過酸化水
素、オゾンが供給されることで、有機物の電解を促進す
る特に酸化力の強いＯＨラジカル（・ＯＨ）の生成量が
増加される。When such a configuration is adopted, the supply of hydrogen peroxide and ozone increases the amount of OH radicals (.OH) that promote electrolysis of organic substances, and particularly have a strong oxidizing power.
【００２２】また、本発明による水処理装置は、陽極と
陰極を備え、汚染物質を含有し供給される被処理水を電
解処理する電解槽と、この電解槽に供給された浮遊固体
と、被処理水及び浮遊固体を流動化させる流動化手段
と、を備えている。Further, the water treatment apparatus according to the present invention has an anode and a cathode, and has an electrolyzer for electrolyzing water to be treated containing pollutants, a suspended solid supplied to the electrolyzer, and an electrolyzer. Fluidizing means for fluidizing the treated water and the suspended solids.
【００２３】このように構成された水処理装置によれ
ば、流動化手段により電解槽の被処理水及び浮遊固体が
流動化されるため、上記水処理方法が効果的に実施され
る。According to the water treatment apparatus configured as described above, since the water to be treated and the suspended solids in the electrolytic cell are fluidized by the fluidizing means, the above-described water treatment method is effectively performed.
【００２４】[0024]
【発明の実施の形態】以下、本発明に係る水処理方法を
適用した水処理装置の好適な実施形態について添付図面
を参照しながら説明する。なお、各図において、同一の
要素には同一の符号を付し、重複する説明は省略する。DESCRIPTION OF THE PREFERRED EMBODIMENTS Preferred embodiments of a water treatment apparatus to which a water treatment method according to the present invention is applied will be described below with reference to the accompanying drawings. In each of the drawings, the same elements are denoted by the same reference numerals, and redundant description will be omitted.
【００２５】図１は、第１実施形態に係る水処理装置を
示す概略構成図である。図１に示すように、水処理装置
２１は、電解処理を行う陽極３及び陰極４を有すると共
に、これら電極３，４の表面を洗浄するための浮遊固体
Ａ（詳しくは後述）が投入されている電解槽５を備え
る。この電解槽５には、被処理水１を供給する被処理水
供給ラインＬ１が接続されると共に、当該電解槽５で電
解処理した処理水を、スクリーン等の分離器９を通すこ
とで浮遊固体Ａと分離して取り出す処理水ラインＬ３が
接続されている。FIG. 1 is a schematic configuration diagram showing a water treatment apparatus according to the first embodiment. As shown in FIG. 1, the water treatment apparatus 21 has an anode 3 and a cathode 4 for performing an electrolytic treatment, and a floating solid A (to be described in detail later) for cleaning the surfaces of the electrodes 3 and 4 is supplied thereto. The electrolytic cell 5 is provided. A treated water supply line L1 for supplying the treated water 1 is connected to the electrolytic tank 5, and the treated water subjected to the electrolytic treatment in the electrolytic tank 5 is passed through a separator 9 such as a screen to form a floating solid. A treated water line L3 which is separated and taken out from A is connected.
【００２６】被処理水供給ラインＬ１は、ダイオキシン
類、環境ホルモン物質等の汚染物質（有害物質）を含有
する被処理水１を電解槽５に供給する。The treated water supply line L 1 supplies treated water 1 containing pollutants (hazardous substances) such as dioxins and environmental hormones to the electrolytic cell 5.
【００２７】電解槽５の陽極３及び陰極４は、板状を成
して対向配置され、複数枚の陽極３、陰極４が交互に位
置するように並設されている。これらの電極３，４は、
被処理水供給ラインＬ１を介して電解槽５に供給される
被処理水１に浸漬されると共に、外部直流電源２に接続
されている。なお、この板状電極に代えて、例えば、網
状、格子状、パイプ状、ハニカム状等の他形状の電極を
用いることも可能である。また、これら電極３，４の材
質としては、特に制限はないが、例えば、白金、銀、白
金族金属を被覆した各種金属、鉄、銅、ニッケル、ステ
ンレス、チタン、炭素等が採用される。The anode 3 and the cathode 4 of the electrolytic cell 5 are arranged opposite to each other in a plate shape, and a plurality of anodes 3 and cathodes 4 are juxtaposed so as to be alternately located. These electrodes 3, 4 are
It is immersed in the water 1 to be supplied to the electrolytic cell 5 via the water supply line L 1, and is connected to the external DC power supply 2. Note that, instead of the plate-like electrode, for example, an electrode of another shape such as a mesh shape, a grid shape, a pipe shape, or a honeycomb shape can be used. The materials of the electrodes 3 and 4 are not particularly limited, and for example, platinum, silver, various metals coated with a platinum group metal, iron, copper, nickel, stainless steel, titanium, carbon and the like are employed.
【００２８】電解槽５の電極３，４より下方の底部に
は、散気管６が設置され、この散気管６には、ガス供給
ラインＬ２を介してブロワ７が接続されている。この散
気管６は、ブロワ７から空気が供給されることで散気口
６ａから空気を散気し、電解槽５の被処理水１中に気泡
Ｂを発生させる。この気泡Ｂにより、水流が発生し被処
理水１が流動化される。An air diffuser 6 is provided below the electrodes 3 and 4 of the electrolytic cell 5 and a blower 7 is connected to the air diffuser 6 via a gas supply line L2. When air is supplied from the blower 7, the air diffuser 6 diffuses the air from the air diffuser port 6 a, and generates bubbles B in the water 1 to be treated in the electrolytic cell 5. Due to the bubbles B, a water flow is generated, and the water to be treated 1 is fluidized.
【００２９】特に、本実施形態においては、電解槽５に
上記浮遊固体Ａが添加されている。この浮遊固体Ａは、
本実施形態では、電解槽５に対する被処理水１の供給前
に予め供給されている。この浮遊固体Ａとしては、例え
ば、プラスチック（ポリプロピレン、ポリスチレン
等）、活性炭、ゼオライト等の鉱物、軽石、砂、珪石、
アルミナ、その他各種のセラミックや各種金属粒等が採
用され、この浮遊固体Ａの形状としては、例えば、球
状、粒状、柱状、中空状、破砕状等各種形状のものが採
用されるが、これらの材質、形状に限定されるものでは
なく、上記散気により被処理水１と共に流動化し得るも
のであれば良く、加えて、電解槽５から取り出される処
理水に対して分離器９で分離回収するのが容易なもので
あれば良い。このため、浮遊固体Ａは、材質によって異
なるが、数ｍｍ〜数ｃｍ程度のものが採用される。な
お、上記ブロワ７、ガス供給ラインＬ２、散気管６によ
り、被処理水１及び浮遊固体Ａを流動化させる流動化手
段が構成されている。In particular, in the present embodiment, the above-mentioned suspended solid A is added to the electrolytic cell 5. This suspended solid A is
In the present embodiment, the water 1 is supplied before the water 1 to be supplied to the electrolytic cell 5. Examples of the suspended solid A include plastics (polypropylene, polystyrene, etc.), activated carbon, minerals such as zeolite, pumice, sand, quartzite,
Alumina, other various ceramics, various metal particles, and the like are employed. As the shape of the suspended solid A, various shapes such as a sphere, a particle, a column, a hollow, and a crushed shape are employed. The material and shape are not limited, and any material may be used as long as it can be fluidized together with the water to be treated 1 by the above-mentioned aeration. In addition, the treated water taken out from the electrolytic cell 5 is separated and collected by the separator 9. Anything that is easy can be used. For this reason, the suspended solid A has a size of about several mm to several cm, although it depends on the material. The blower 7, the gas supply line L2, and the air diffuser 6 constitute fluidizing means for fluidizing the water 1 to be treated and the suspended solids A.
【００３０】電極３，４同士の間隔は、気泡Ｂにより発
生する水流と浮遊固体Ａの流動化を高める必要があるこ
と、水の電気抵抗があまり高くなると電力費が嵩むこと
等を考慮して、数ｃｍ〜数十ｃｍの比較的狭い極間距離
に設定されている。また、直流電源２の電圧は、数Ｖ〜
数十Ｖ、電流密度は数Ａ／ｍ2〜数百Ａ／ｍ2程度にされ
ている。The distance between the electrodes 3 and 4 is determined in consideration of the necessity of increasing the flow of the water flow generated by the bubbles B and the fluidization of the suspended solid A, and the fact that the electric resistance of water becomes too high increases the power cost. , And a relatively narrow distance between the poles of several cm to several tens cm. The voltage of the DC power supply 2 is several volts or more.
Several tens of volts and a current density of about several A / m 2 to several hundred A / m 2 are set.
【００３１】このような水処理装置２１によれば、浮遊
固体Ａが予め添加されている電解槽５に、被処理水１が
被処理水供給ラインＬ１を介して供給され、電極３，４
が通電されることで、被処理水１が電解処理される。According to the water treatment apparatus 21, the water 1 to be treated is supplied to the electrolytic cell 5 to which the suspended solid A has been added in advance through the water supply line L 1.
Is supplied with electricity, the water 1 to be treated is subjected to electrolytic treatment.
【００３２】この時、ブロワ７の駆動による散気によっ
て被処理水１には気泡Ｂが発生し、この気泡Ｂにより発
生する水流によって、被処理水１が流動化されると共に
浮遊固体Ａが流動化される。At this time, bubbles B are generated in the water 1 to be treated by the air diffused by the drive of the blower 7, and the water flow generated by the bubbles B fluidizes the water 1 and causes the floating solids A to flow. Be transformed into
【００３３】従って、浮遊固体Ａが電極３，４に対して
衝突し、これにより、当該電極３，４の付着物が効果的
に剥離される。加えて、気泡Ｂにより形成される水流で
も電極３，４が洗浄される。特に、本実施形態では、電
極３，４が比較的狭い間隔で配置されているため、水流
及び浮遊固体Ａの流れが強く、電極３，４の付着物が一
層効果的に剥離される。Therefore, the floating solid A collides with the electrodes 3 and 4, whereby the deposits on the electrodes 3 and 4 are effectively peeled off. In addition, the electrodes 3 and 4 are also washed by the water flow formed by the bubbles B. In particular, in the present embodiment, since the electrodes 3 and 4 are arranged at relatively small intervals, the flow of the water and the suspended solid A is strong, and the deposits on the electrodes 3 and 4 are more effectively separated.
【００３４】ここで、浮遊固体Ａの電解槽５への添加量
は、容積比で０．５％〜３０％が好ましい。これは、
０．５％より小さいと、電極３，４の付着物の剥離効果
が不十分であり、３０％を越えると、電極３，４間で閉
塞が生じたり、浮遊固体Ａの流動化が困難になるからで
ある。Here, the amount of the suspended solid A added to the electrolytic cell 5 is preferably 0.5% to 30% by volume. this is,
If it is less than 0.5%, the effect of removing the deposits on the electrodes 3 and 4 is insufficient, and if it exceeds 30%, clogging occurs between the electrodes 3 and 4 or fluidization of the suspended solid A becomes difficult. Because it becomes.
【００３５】このように、電解槽５では効果的に電極
３，４が洗浄されるため、電解処理が経時的に良好に成
される。この電解槽５で良好に電解処理された処理水
は、分離器９で浮遊固体Ａと分離され処理水ラインＬ３
を介して取り出される。この処理水は、放流若しくは再
利用されるが、必要に応じてさらに別工程の処理が実施
される。As described above, since the electrodes 3 and 4 are effectively washed in the electrolytic cell 5, the electrolytic treatment is favorably performed with time. The treated water satisfactorily electrolyzed in the electrolytic cell 5 is separated from the suspended solid A in the separator 9 and the treated water line L3
Is taken out through. This treated water is discharged or reused, but a further process is performed if necessary.
【００３６】なお、浮遊固体Ａを分離器９で分離回収す
るのではなく、次工程として例えば浮上分離、沈殿分
離、膜分離等を設定し、ここで浮遊固体Ａを分離回収し
て電解槽５に戻すようにしても良い。The floating solid A is not separated and recovered by the separator 9, but, for example, flotation, sedimentation, and membrane separation are set as the next step. May be returned.
【００３７】このように、本実施形態においては、汚染
物質を含有する被処理水１と浮遊固体Ａが流動化される
ため、この流動化する浮遊固体Ａが電極３，４に衝突し
当該電極３，４の付着物が効果的に剥離されるようにな
っている。このため、電極３，４が十分に洗浄され、電
気分解を経時的に安定して行うことが可能とされてい
る。As described above, in the present embodiment, the water 1 to be treated containing the contaminant and the floating solid A are fluidized, and the fluidized floating solid A collides with the electrodes 3 and 4 and the floating solid A The deposits 3 and 4 are effectively peeled off. Therefore, the electrodes 3 and 4 are sufficiently washed, and the electrolysis can be stably performed with time.
【００３８】また、本実施形態においては、被処理水１
及び浮遊固体Ａの流動化が、撹拌翼等の機械的手段では
なく空気供給（ガス供給）により実施されているため、
電解槽５の簡素化が図られている。このため、電解槽５
の小型化及び低コスト化が可能とされている。In this embodiment, the water 1 to be treated is
And the fluidization of the suspended solid A is carried out by air supply (gas supply) instead of mechanical means such as a stirring blade,
The electrolytic cell 5 is simplified. Therefore, the electrolytic cell 5
It is possible to reduce the size and cost of the device.
【００３９】ここで、電解槽５に、過酸化水素及びオゾ
ンの少なくとも一方を供給して被処理水１を電解処理す
るのが好ましい。このように過酸化水素、オゾンを供給
すると、有機物の電解を促進する特に酸化力の強いＯＨ
ラジカル（・ＯＨ）の生成量が増加されるため、汚染物
質の分解が一層促進されることになる。Here, it is preferable that at least one of hydrogen peroxide and ozone is supplied to the electrolytic cell 5 to electrolyze the water 1 to be treated. Supplying hydrogen peroxide and ozone in this way promotes electrolysis of organic substances, especially OH having a strong oxidizing power.
Since the amount of generated radicals (.OH) is increased, the decomposition of pollutants is further promoted.
【００４０】なお、被処理水１の電気伝導度が低い場合
には、Ｎａ、Ｋ等の化合物（例えば塩化物）を添加して
も良い。また、散気管６から供給される空気に代えて、
オゾン含有の空気や酸素ガス等を用いても良い。さらに
また、ｐＨを調整すべく、酸やアルカリを添加しても良
い。When the electric conductivity of the water 1 to be treated is low, compounds such as Na and K (for example, chlorides) may be added. Also, instead of the air supplied from the air diffuser 6,
Ozone-containing air or oxygen gas may be used. Furthermore, an acid or an alkali may be added to adjust the pH.
【００４１】図２は、本発明の第２実施形態に係る水処
理装置を示す概略構成図である。この第２実施形態の水
処理装置３１が第１実施形態の水処理装置２１と違う点
は、電解槽５に生物汚泥（活性汚泥）Ｃを投入している
点である。FIG. 2 is a schematic configuration diagram showing a water treatment apparatus according to a second embodiment of the present invention. The difference between the water treatment apparatus 31 of the second embodiment and the water treatment apparatus 21 of the first embodiment is that biological sludge (activated sludge) C is supplied to the electrolytic cell 5.
【００４２】この生物汚泥Ｃは、有機物を分解するもの
であり、その濃度は、生物汚泥法の場合と同様の０．１
〜１％程度にされている。This biological sludge C is for decomposing organic substances, and its concentration is 0.1% as in the case of the biological sludge method.
About 1%.
【００４３】また、この第２実施形態では、当該生物汚
泥Ｃが分離器９を通過して処理水と共に処理水ラインＬ
３を流れるため、この処理水ラインＬ３を流れる生物汚
泥Ｃを電解槽５に戻す返送システムが付設されている。
この返送システムでは、処理水ラインＬ３に接続された
沈殿槽１０で、生物汚泥Ｃが沈殿して処理水と分離さ
れ、この沈殿汚泥１２が返送ラインＬ５を介して電解槽
５に返送され、一方、上澄の処理水が処理水ラインＬ４
を介して取り出されるように成されている。なお、沈殿
汚泥１２が浮上するのを防止するために、処理水ライン
Ｌ３の途中に脱気装置を設けると良い。In the second embodiment, the biological sludge C passes through the separator 9 and the treated water line L together with the treated water.
3, a return system for returning the biological sludge C flowing through the treated water line L3 to the electrolytic tank 5 is provided.
In this return system, biological sludge C precipitates and is separated from treated water in the settling tank 10 connected to the treated water line L3, and the settled sludge 12 is returned to the electrolytic tank 5 through the return line L5. , The supernatant treated water is in treated water line L4
To be taken out. In order to prevent the settling sludge 12 from floating, a deaerator may be provided in the middle of the treated water line L3.
【００４４】このような第２実施形態によれば、電解槽
５に生物汚泥Ｃが共存しているため、電解槽の機能に加
えて、有機物を分解する生物汚泥槽としての機能も有し
ており、この生物汚泥Ｃにより、汚染物質の分解が一層
促進されるようになっている。According to the second embodiment, since the biological sludge C coexists in the electrolytic cell 5, in addition to the function of the electrolytic cell, it has a function as a biological sludge tank for decomposing organic substances. The decomposition of pollutants is further promoted by the biological sludge C.
【００４５】また、生物汚泥Ｃに必要な酸素（空気）
が、被処理水１及び浮遊固体Ａを流動化させるべく、ブ
ロワ７からガス供給ラインＬ２、散気管６、散気口６ａ
を介して供給されているため、生物汚泥Ｃ用に別途酸素
を供給するのが不要とされており、電解槽５の低コスト
化が可能とされている。The oxygen (air) required for the biological sludge C
However, in order to fluidize the water 1 to be treated and the suspended solid A, a gas supply line L2, a diffuser 6 and a diffuser 6a are provided from the blower 7.
Therefore, it is not necessary to separately supply oxygen for the biological sludge C, and the cost of the electrolytic cell 5 can be reduced.
【００４６】なお、生物汚泥Ｃの分離は、図２に示す沈
殿分離に限定されるものではなく、例えば浮上分離や膜
分離等であっても良い。Incidentally, the separation of the biological sludge C is not limited to the sedimentation separation shown in FIG. 2, but may be, for example, flotation separation or membrane separation.
【００４７】また、この第２実施形態でも、過酸化水素
及びオゾンの少なくとも一方を供給するようにすれば、
汚染物質の分解がより一層促進されることになる。Also in the second embodiment, if at least one of hydrogen peroxide and ozone is supplied,
The decomposition of pollutants will be further promoted.
【００４８】ここで、本発明者らは、上述の効果を確認
すべく、以下の実施例１〜３、比較例１の条件で実験を
実施した。Here, the present inventors conducted experiments under the following conditions of Examples 1 to 3 and Comparative Example 1 in order to confirm the above effects.
【００４９】（実施例１）ダイオキシン類を２０ｐｇＴ
ＥＱ／ｌ含有するごみの埋め立て浸出水を被処理水とし
て、毎時９ｌの割合で、粒径約３ｍｍφの多孔性セラミ
ット（浮遊固体：セラミック粒子）が容積比で３％添加
された有効容積が９ｌの電解槽（３０×１０×４０ｃｍ
高さ）に連続的に供給した。電解槽には、白金鍍金チタ
ン板の陽極とステンレス板の陰極（何れの電極もサイズ
は２５×８×０．０５ｃｍ厚さ）を、極間６ｃｍ間隔で
２枚づつ、計４枚を配置した。電解を開始した時点から
槽底部全面より毎分１ｌの空気を供給して、電解を１０
００時間実施した。電解槽の出口側には、セラミック粒
子の流出を防止する約２ｍｍのスクリーンを設置した。
その結果、電極の汚れは比較的少なく、１０００時間後
でも同じ電解電圧で電流値は５％低下しただけであっ
た。また、処理水のダイオキシンを分析した結果、当初
の除去率７０％に対して１０００時間後でも６８％の除
去率が得られた。すなわち、電気分解を経時的に安定し
て行い得るのが確認された。Example 1 Dioxins were converted to 20 pgT
The landfill leachate of the garbage containing EQ / l is treated water, and the effective volume to which 3% by volume of a porous ceramite (suspended solid: ceramic particles) having a particle diameter of about 3 mmφ is added is 9 liters / hour. Electrolytic cell (30 × 10 × 40cm
(Height) continuously. In the electrolytic cell, a total of four anodes of a platinum-plated titanium plate and two cathodes of a stainless steel plate (each electrode having a size of 25 × 8 × 0.05 cm thick) were arranged at intervals of 6 cm between the electrodes. . From the start of electrolysis, air was supplied at a rate of 1 liter per minute from the entire bottom of the tank to perform electrolysis for 10 minutes.
The test was performed for 00 hours. On the outlet side of the electrolytic cell, a screen of about 2 mm for preventing outflow of ceramic particles was provided.
As a result, contamination of the electrode was relatively small, and the current value decreased only 5% at the same electrolytic voltage even after 1000 hours. In addition, as a result of analyzing dioxin in the treated water, a removal rate of 68% was obtained even after 1000 hours, compared to an initial removal rate of 70%. That is, it was confirmed that the electrolysis could be stably performed over time.
【００５０】（比較例１）セラミック粒子を添加しない
以外は、実施例１と同じ条件で電解処理した。その結
果、１０００時間後の電解電流は当初の２０％と大幅に
低下し、ダイオキシン除去率も１５％と大幅に低下し
た。すなわち、セラミック粒子を添加しない電解処理で
は、電気分解を経時的に安定して行うのが困難であっ
た。(Comparative Example 1) Electrolysis was performed under the same conditions as in Example 1 except that no ceramic particles were added. As a result, the electrolysis current after 1000 hours was greatly reduced to the initial 20%, and the dioxin removal rate was also significantly reduced to 15%. That is, in the electrolytic treatment without adding the ceramic particles, it was difficult to stably perform the electrolysis over time.
【００５１】（実施例２）実施例１の電解槽底部より供
給する空気を、オゾンを０．１％含有する空気に代え
て、実施例１と同様に電解処理した。その結果、電極の
汚れは少なく、１０００時間後でも同じ電解電圧で電流
値は５％低下しただけであった。また、ダイオキシン除
去率は、当初の除去率９５％に対して１０００時間後で
も９３％の除去率が得られた。すなわち、電気分解を経
時的に安定して行い得ると共に、オゾンの存在により、
ダイオキシン除去率が向上するのが確認された。(Example 2) Electrolysis was performed in the same manner as in Example 1 except that the air supplied from the bottom of the electrolytic cell in Example 1 was replaced with air containing 0.1% of ozone. As a result, the electrode was less contaminated, and the current value decreased only 5% at the same electrolytic voltage even after 1000 hours. The dioxin removal rate was 93% even after 1000 hours, compared to the initial removal rate of 95%. That is, while the electrolysis can be performed stably with time, and the presence of ozone,
It was confirmed that the dioxin removal rate was improved.
【００５２】（実施例３）実施例１の電解槽に、生物汚
泥を５０００ｍｇ／ｌ共存させて、実施例１と同様に電
解処理した。但し、生物汚泥はスクリーンで分離回収で
きないので、次工程で沈殿分離して回収し、電解槽に戻
して生物汚泥を５０００ｍｇ／ｌに保持するようにし
た。その結果、被処理水のＢＯＤが５０ｐｐｍに対して
処理水のそれは８ｐｐｍであった。また、生物汚泥を共
存させない条件下では、処理水のＢＯＤは２０ｐｐｍで
あった。すなわち、生物汚泥の存在により、ＢＯＤの除
去性能が向上するのが確認された。(Example 3) In the electrolytic cell of Example 1, an electrolytic treatment was carried out in the same manner as in Example 1, except that 5000 mg / l of biological sludge coexisted. However, since the biological sludge cannot be separated and recovered by a screen, the biological sludge is separated and recovered in the next step, and is returned to the electrolytic cell to maintain the biological sludge at 5000 mg / l. As a result, the BOD of the treated water was 8 ppm while the BOD of the treated water was 50 ppm. In addition, the BOD of the treated water was 20 ppm under the condition that no biological sludge coexisted. That is, it was confirmed that the removal performance of BOD was improved by the presence of biological sludge.
【００５３】以上、本発明をその実施形態に基づき具体
的に説明したが、本発明は上記実施形態に限定されるも
のではなく、例えば、上記実施形態においては、電解槽
５の簡素化を図るべく、ガスを供給して、被処理水１及
び浮遊固体Ａを流動化させるようにしているが、撹拌翼
等の機械的手段により流動化させることも可能である。As described above, the present invention has been specifically described based on the embodiment. However, the present invention is not limited to the above embodiment. For example, in the above embodiment, the electrolytic cell 5 is simplified. For this purpose, gas is supplied to fluidize the water 1 to be treated and the suspended solids A, but fluidization can also be carried out by mechanical means such as a stirring blade.
【００５４】また、生物汚泥Ｃを電解槽５に共存させる
場合には、供給ガスを空気等の酸素含有ガスとする必要
があるが、生物汚泥Ｃを電解槽５に共存させない場合に
は、供給ガスは酸素含有ガスに限定されるものではな
い。When the biological sludge C is allowed to coexist in the electrolytic cell 5, the supply gas needs to be an oxygen-containing gas such as air. The gas is not limited to an oxygen-containing gas.
【００５５】また、電極３，４の汚れ、特に陰極４に対
する非導電物質の析出、陽極３に対する酸化膜の生成を
防止すべく、直流電源２の電極３，４に対する供給ライ
ンに極性反転スイッチを介装し、陽極３と陰極４の極性
を定期的に交替して運転するようにしても良い。In order to prevent contamination of the electrodes 3 and 4, in particular, deposition of a non-conductive substance on the cathode 4 and formation of an oxide film on the anode 3, a polarity inversion switch is provided in the supply line for the electrodes 3 and 4 of the DC power supply 2. The operation may be performed by interposing the anode 3 and the cathode 4 while periodically changing the polarity.
【００５６】また、上記実施例においては、電解槽５に
予め浮遊固体Ａを供給するようにしているが、例えば、
直流電源２の電極３，４に対する供給ラインに電流計を
介装し、この電流計を例えばコンピュータにより監視す
ることで電極３，４の汚れの度合いを検出し、電流値が
所定値以下に低下したら当該電極３，４が所定に汚れと
判断して、浮遊固体Ａを電解槽５に供給するようにして
も良い。このようにすることで、陽極３からの金属の溶
出を防止すべく当該陽極３に例えば白金等の鍍金を施し
ている場合には、この鍍金に対する浮遊固体Ａの衝突の
機会が必要最低限とされて、当該鍍金の剥離の虞が低減
され、電気分解が経時的に一層安定して行われることに
なる。また、鍍金に対する浮遊固体Ａの衝突の機会を必
要最低限とすべく、浮遊固体Ａを定期的に電解槽５に供
給しても良い。In the above embodiment, the suspended solid A is supplied to the electrolytic cell 5 in advance.
An ammeter is interposed in the supply line for the electrodes 3 and 4 of the DC power supply 2, and the degree of contamination of the electrodes 3 and 4 is detected by monitoring the ammeter with a computer, for example, and the current value falls below a predetermined value. Then, the electrodes 3 and 4 may be determined to be contaminated in a predetermined manner, and the suspended solid A may be supplied to the electrolytic cell 5. In this way, when the anode 3 is plated with, for example, platinum or the like in order to prevent the elution of metal from the anode 3, the chance of collision of the suspended solid A with the plating is minimized. Then, the fear of peeling of the plating is reduced, and the electrolysis is performed more stably with time. Further, the floating solid A may be supplied to the electrolytic cell 5 periodically so as to minimize the chance of the collision of the floating solid A with the plating.
【００５７】さらにまた、例えばアルミニウム、鉄等の
溶解性電極を陽極３に用いるようにすれば、被処理水の
燐酸イオンと反応して不溶性の燐酸塩が生成されること
になり、富栄養化で問題になっている燐を除去すること
も可能である。Furthermore, if a soluble electrode of, for example, aluminum or iron is used for the anode 3, it reacts with the phosphate ions of the water to be treated to form insoluble phosphates, thereby increasing eutrophication. It is also possible to remove the problematic phosphorus.
【００５８】[0058]
【発明の効果】本発明による水処理方法及び水処理装置
は、陽極と陰極を備える電解槽に、汚染物質を含有する
被処理水を供給し、電解槽に供給された浮遊固体と共に
被処理水を流動化させて当該被処理水を電解処理してい
るため、流動化する浮遊固体が電極に衝突し当該電極の
付着物が効果的に剥離される。このため、電極が十分に
洗浄され、電気分解を経時的に安定して行うことが可能
となる。According to the water treatment method and the water treatment apparatus of the present invention, the water to be treated containing contaminants is supplied to an electrolytic cell having an anode and a cathode, and the water to be treated is treated together with the suspended solid supplied to the electrolytic cell. Is fluidized and the water to be treated is subjected to the electrolytic treatment, so that the floating solid that is fluidized collides with the electrode, and the deposits on the electrode are effectively peeled off. Therefore, the electrodes are sufficiently washed, and the electrolysis can be stably performed with time.
【図１】本発明の第１実施形態に係る水処理装置を示す
概略構成図である。FIG. 1 is a schematic configuration diagram showing a water treatment device according to a first embodiment of the present invention.
【図２】本発明の第２実施形態に係る水処理装置を示す
概略構成図である。FIG. 2 is a schematic configuration diagram illustrating a water treatment device according to a second embodiment of the present invention.
１…被処理水、２…電源、３…陽極、４…陰極、５…電
解槽、６…散気管（流動化手段）、７…ブロワ（流動化
手段）、２１，３１…水処理装置、Ａ…浮遊固体、Ｂ…
気泡、Ｃ…生物汚泥、Ｌ２…ガス供給ライン（流動化手
段）。DESCRIPTION OF SYMBOLS 1 ... Water to be processed, 2 ... Power supply, 3 ... Anode, 4 ... Cathode, 5 ... Electrolyzer, 6 ... Aerator (fluidizing means), 7 ... Blower (fluidizing means), 21, 31 ... Water treatment apparatus A: suspended solid, B:
Bubble, C: biological sludge, L2: gas supply line (fluidizing means).
───────────────────────────────────────────────────── フロントページの続き Ｆターム(参考） 4D028 AB00 BC12 BD06 4D050 AA13 AA15 AB19 BB02 BB09 CA10 4D061 DA08 DB19 DC08 EA03 EB01 EB04 EB20 EB27 EB28 EB29 EB30 EB33 EB35 EB37 ED12 ED20 FA15 GA30 ──────────────────────────────────────────────────続 き Continued on the front page F term (reference) 4D028 AB00 BC12 BD06 4D050 AA13 AA15 AB19 BB02 BB09 CA10 4D061 DA08 DB19 DC08 EA03 EB01 EB04 EB20 EB27 EB28 EB29 EB30 EB33 EB35 EB37 ED12 ED20 FA15 GA30
Claims (7)
を含有する被処理水を供給し、 前記電解槽に供給された浮遊固体と共に前記被処理水を
流動化させて当該被処理水を電解処理することを特徴と
する水処理方法。1. An untreated water containing a contaminant is supplied to an electrolytic cell having an anode and a cathode, and the untreated water is fluidized together with the suspended solid supplied to the electrolytic cell to remove the untreated water. A water treatment method characterized by performing an electrolytic treatment.
に予め前記電解槽に供給することを特徴とする請求項１
記載の水処理方法。2. The method according to claim 1, wherein the suspended solid is supplied to the electrolytic cell in advance before supplying the water to be treated.
Water treatment method as described.
に供給することを特徴とする請求項１記載の水処理方
法。3. The water treatment method according to claim 1, wherein the degree of contamination of the electrode is detected, and when the electrode is contaminated to a predetermined degree, the suspended solid is supplied to the electrolytic cell.
理水及び前記浮遊固体を流動化させることを特徴とする
請求項１〜３の何れか一項に記載の水処理方法。4. The water treatment method according to claim 1, wherein a gas is supplied to the electrolytic cell to fluidize the water to be treated and the suspended solid.
処理することを特徴とする請求項４記載の水処理方法。5. The water treatment method according to claim 4, wherein the gas is an oxygen-containing gas, and the water to be treated is subjected to electrolytic treatment in the presence of biological sludge in the electrolytic cell.
少なくとも一方を供給して前記被処理水を電解処理する
ことを特徴とする請求項１〜５の何れか一項に記載の水
処理方法。6. The water treatment according to claim 1, wherein at least one of hydrogen peroxide and ozone is supplied to the electrolysis tank to electrolyze the water to be treated. Method.
給される被処理水を電解処理する電解槽と、この電解槽
に供給された浮遊固体と、 前記被処理水及び前記浮遊固体を流動化させる流動化手
段と、を備える水処理装置。7. An electrolytic cell, comprising an anode and a cathode, for electrolytically treating water to be supplied containing a contaminant, floating solids supplied to the electrolytic cell, and the water to be treated and the floating solids. And a fluidizing means for fluidizing.
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000208643A JP2002018443A (en) | 2000-07-10 | 2000-07-10 | Method and apparatus for water treatment |
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| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2000208643A JP2002018443A (en) | 2000-07-10 | 2000-07-10 | Method and apparatus for water treatment |
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|---|---|
| JP2002018443A true JP2002018443A (en) | 2002-01-22 |
Family
ID=18705193
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|---|---|---|---|
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Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004069754A1 (en) * | 2003-02-10 | 2004-08-19 | Nt Nitto Sangyo Co., Ltd | Method of decomposing hardly decomposable organic compound and apparatus therefor |
| WO2005049502A1 (en) * | 2003-11-19 | 2005-06-02 | Anzai, Setsu | Waste water treating system for treating waste water after biogas is produced |
| CN105800739A (en) * | 2016-05-27 | 2016-07-27 | 长沙华时捷环保科技发展股份有限公司 | 3D-EO three-dimensional peroxidation electrochemical device and application thereof |
-
2000
- 2000-07-10 JP JP2000208643A patent/JP2002018443A/en active Pending
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| WO2004069754A1 (en) * | 2003-02-10 | 2004-08-19 | Nt Nitto Sangyo Co., Ltd | Method of decomposing hardly decomposable organic compound and apparatus therefor |
| WO2005049502A1 (en) * | 2003-11-19 | 2005-06-02 | Anzai, Setsu | Waste water treating system for treating waste water after biogas is produced |
| CN105800739A (en) * | 2016-05-27 | 2016-07-27 | 长沙华时捷环保科技发展股份有限公司 | 3D-EO three-dimensional peroxidation electrochemical device and application thereof |
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