JPH04131185A - Electric floating device - Google Patents
Electric floating deviceInfo
- Publication number
- JPH04131185A JPH04131185A JP24969290A JP24969290A JPH04131185A JP H04131185 A JPH04131185 A JP H04131185A JP 24969290 A JP24969290 A JP 24969290A JP 24969290 A JP24969290 A JP 24969290A JP H04131185 A JPH04131185 A JP H04131185A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- floc
- waste water
- gas bubbles
- flocs
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Pending
Links
- 239000002351 wastewater Substances 0.000 claims abstract description 61
- 238000005188 flotation Methods 0.000 claims description 46
- 238000005339 levitation Methods 0.000 claims description 22
- 238000006243 chemical reaction Methods 0.000 claims description 13
- 238000000926 separation method Methods 0.000 claims description 7
- 238000011144 upstream manufacturing Methods 0.000 claims 1
- UFHFLCQGNIYNRP-UHFFFAOYSA-N Hydrogen Chemical compound [H][H] UFHFLCQGNIYNRP-UHFFFAOYSA-N 0.000 abstract description 16
- 239000010802 sludge Substances 0.000 abstract description 9
- 238000005868 electrolysis reaction Methods 0.000 abstract description 6
- 238000006479 redox reaction Methods 0.000 abstract description 5
- 238000004040 coloring Methods 0.000 abstract 1
- 238000000034 method Methods 0.000 description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 23
- 238000007130 inorganic reaction Methods 0.000 description 17
- 239000007789 gas Substances 0.000 description 11
- 229920000642 polymer Polymers 0.000 description 8
- 238000004065 wastewater treatment Methods 0.000 description 7
- 230000000694 effects Effects 0.000 description 6
- 239000000049 pigment Substances 0.000 description 6
- 238000003756 stirring Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- WQYVRQLZKVEZGA-UHFFFAOYSA-N hypochlorite Chemical compound Cl[O-] WQYVRQLZKVEZGA-UHFFFAOYSA-N 0.000 description 4
- 238000012545 processing Methods 0.000 description 4
- 238000005516 engineering process Methods 0.000 description 3
- 239000003344 environmental pollutant Substances 0.000 description 3
- 244000144992 flock Species 0.000 description 3
- 230000002209 hydrophobic effect Effects 0.000 description 3
- 231100000719 pollutant Toxicity 0.000 description 3
- KZBUYRJDOAKODT-UHFFFAOYSA-N Chlorine Chemical compound ClCl KZBUYRJDOAKODT-UHFFFAOYSA-N 0.000 description 2
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 2
- 238000005273 aeration Methods 0.000 description 2
- 230000003197 catalytic effect Effects 0.000 description 2
- 230000007423 decrease Effects 0.000 description 2
- 239000010842 industrial wastewater Substances 0.000 description 2
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 2
- 230000003647 oxidation Effects 0.000 description 2
- 238000007254 oxidation reaction Methods 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 238000001223 reverse osmosis Methods 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 238000001179 sorption measurement Methods 0.000 description 2
- 238000004458 analytical method Methods 0.000 description 1
- 230000033228 biological regulation Effects 0.000 description 1
- 239000010782 bulky waste Substances 0.000 description 1
- 239000006227 byproduct Substances 0.000 description 1
- 239000003795 chemical substances by application Substances 0.000 description 1
- 238000004042 decolorization Methods 0.000 description 1
- 238000013461 design Methods 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 238000010586 diagram Methods 0.000 description 1
- 239000003657 drainage water Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 238000010979 pH adjustment Methods 0.000 description 1
- 239000002245 particle Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 238000003672 processing method Methods 0.000 description 1
- 102000004169 proteins and genes Human genes 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 238000006722 reduction reaction Methods 0.000 description 1
- 235000014102 seafood Nutrition 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 238000010257 thawing Methods 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Water Treatment By Electricity Or Magnetism (AREA)
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、産業排水の処理技術に関し、特に電気浮上法
を利用した有機排水処理に適用して有効な技術に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a technology for treating industrial wastewater, and in particular to a technology that is effective when applied to organic wastewater treatment using electric levitation.
産業排水の処理方法には、大別して生物的処理方法と物
理化学的処理方法とがあり、有機排水の処理には、主と
して（１）活性汚泥法、（２）接触酸化法、（３〕円板
曝気法などの生物的処理方法が利用されている。しかし
、生物的処理方法は、処理ＢＯＤ １ｋｇ／日に対し、
水量０．５〜１ｍ’／日、空気量５ＯＮｍ’／日を必要
とするため、設備面積、施設費などに莫大が経費を要す
る欠点のあることが指摘されている。Treatment methods for industrial wastewater can be roughly divided into biological treatment methods and physicochemical treatment methods.The treatment methods for organic wastewater are mainly (1) activated sludge method, (2) catalytic oxidation method, and (3) catalytic oxidation method. Biological treatment methods such as plate aeration method are used. However, biological treatment methods have a
It has been pointed out that since it requires a water volume of 0.5 to 1 m'/day and an air volume of 5 ONm'/day, it has the drawback of requiring a huge amount of equipment area and facility costs.
一方、物理化学的処理方法には、（１）凝集沈澱法、（
２）加圧浮上法、（３）電気浮上法、（４）吸着法、（
５）逆浸透圧法などがある。これらの処理方法のうち、
吸着法および逆浸透圧法は、生物的処理方法などで処理
された排水をより高度に処理するために利用されている
。凝集沈澱法は、重い粒子を含み、かつ油分を含まない
排水の処理に利用されている。On the other hand, physicochemical treatment methods include (1) coagulation-precipitation method, (
2) Pressure levitation method, (3) Electric levitation method, (4) Adsorption method, (
5) There is a reverse osmosis method. Among these processing methods,
Adsorption methods and reverse osmosis methods are used to more advancedly treat wastewater that has been treated with biological treatment methods. The coagulation-sedimentation method is used to treat wastewater that contains heavy particles but does not contain oil.
加圧浮上法は、高濃度排水中の５５ＳＢＯＤ、Ｃ０Ｄ、
油分などを効率よく除去できることから、生物的処理の
前処理として、また水質規制値があまり厳しくない場合
には単独で利用されている。The pressure flotation method is used to remove 55SBOD, COD, and COD in high concentration wastewater.
Because it can efficiently remove oil and other substances, it is used as a pretreatment for biological treatment, and when water quality regulations are not too strict, it is used alone.
電気浮上法は、■有機排水を無機反応槽および高分子反
応槽に導き、排水中の親永住物質の一部および疎水性汚
濁物質を凝集させてフロックを形成する工程、■フロッ
クを形成した排水を浮上槽に導き、フロックに電解ガス
気泡を会合させて浮上させる工程、■浮上したフロック
を浮上分離槽に導き、スキーマ−によって除去する工程
からなり、加圧浮上法と同様、高濃度排水中の５ＳＳＢ
ＯＤ。Electric levitation is a process in which organic wastewater is introduced into an inorganic reaction tank and a polymer reaction tank, and part of the parent permanent resident substances and hydrophobic pollutants in the wastewater are flocculated to form flocs; The process consists of the following steps: 1. Guide the floated flocs to a flotation tank, make electrolytic gas bubbles associate with the flocs, and float the flocs; 1) Guide the floated flocs to a flotation separation tank and remove them using a schema; 5SSB
O.D.
ＣＯＤ、油分などを効率よく除去できる利点を有してい
る。また、電気浮上法は、加圧浮上法に比べて下記のよ
うな利点を有している。It has the advantage of efficiently removing COD, oil, etc. Furthermore, the electric levitation method has the following advantages over the pressure levitation method.
（１）、コンプレッサーや加圧ポンプを使用しないので
、騒音が発生しない。(1) Since no compressor or pressure pump is used, no noise is generated.
（２）、加圧水を使用しないので、浮上分離槽を小形化
することができる。また、加圧水製造装置を必要としな
いので、設備全体を小形化することができる。(2) Since pressurized water is not used, the flotation tank can be made smaller. Furthermore, since a pressurized water production device is not required, the entire equipment can be downsized.
（３）、電解電流の変動操作により、微細な電解ガス気
泡の増減、制御を容易に行うことができる。(3) By varying the electrolytic current, it is possible to easily control and increase the number of fine electrolytic gas bubbles.
（４）、！解の副次的効果として、次亜塩素ガス、塩素
ガスの副生によるＢＯＤ５Ｃ０Ｄの低減、脱色効果が得
られる。(4),! As a side effect of the solution, a reduction in BOD5C0D and a decolorizing effect can be obtained due to the by-product of hypochlorite gas and chlorine gas.
なお、上記電気浮上法を利用した排水処理装置について
は、特開昭６２−３８２８６号公報、特開平２−２１９
９４号公報などに記載がある。Regarding wastewater treatment equipment using the above-mentioned electric levitation method, Japanese Patent Application Laid-Open No. 62-38286 and Japanese Patent Application Laid-open No. 2-219
There is a description in Publication No. 94, etc.
電気浮上法は、前述したような多くの利点を有する優れ
た排水処理方法であるが、この電気浮上法を利用した従
来の排水処理装置は、下記のような実用上の問題点を有
しているため、有機排水の処理には殆ど利用されていな
いのが現状である。The electric levitation method is an excellent wastewater treatment method that has many advantages as mentioned above, but conventional wastewater treatment equipment that uses this electric levitation method has the following practical problems. Currently, it is hardly used for treating organic wastewater.
（１）、浮上槽における電解ガス気泡の密度が小さいた
と、電解ガス気泡とフロックとの会合が不充分となり、
会合を受けないフロックが多量に発生してキャリオーバ
ー現象が生じる。また、−旦浮上したフロックから電解
ガス気泡が分離、逸散し、フロックが再沈澱し易い。こ
れらの理由により、ＳＳの除去効率が低い。(1) If the density of electrolytic gas bubbles in the flotation tank is low, the association between electrolytic gas bubbles and flocs will be insufficient;
A large amount of flocs that do not undergo association occurs, causing a carryover phenomenon. Moreover, electrolytic gas bubbles separate and dissipate from the flocs that have floated once, and the flocs tend to re-sediment. For these reasons, the SS removal efficiency is low.
（２）、浮上槽に導かれた排水が電極間を通過する際、
フロックによって架橋が形成され易いため、電気的な短
絡が生じて電解ガス気泡の発生が停止する事故が発生す
る。(2) When the wastewater led to the flotation tank passes between the electrodes,
Since crosslinks are easily formed by the flocs, an accident occurs in which an electrical short circuit occurs and the generation of electrolytic gas bubbles is stopped.
（３）、浮上槽の構造上、電極の洗浄やスケール除去が
困難なため、ＳＳの除去効率が経時的に低下する。(3) Due to the structure of the flotation tank, it is difficult to clean the electrodes and remove scale, so the SS removal efficiency decreases over time.
（４）、キャリオーバーによるフロックの発生によって
、ＢＯＤ５Ｃ０Ｄの除去効率も低下する。(4) The removal efficiency of BOD5C0D also decreases due to the occurrence of flocs due to carryover.
本発明の目的は、電気浮上法を利用した排水処理装置（
以下、単に電気浮上装置という）の上記した問題点を改
善し、有機排水を効率的に処理することのできる電気浮
上装置を提供することにある。The purpose of the present invention is to provide a wastewater treatment device (
It is an object of the present invention to provide an electric levitation device which can improve the above-mentioned problems of the electric levitation device (hereinafter simply referred to as an electric levitation device) and can efficiently treat organic wastewater.
本願において開示される発明のうち、代表的なものの概
要を簡単に説明すれば、次のとおりである。A brief overview of typical inventions disclosed in this application is as follows.
本願の一発胡である電気浮上装置は、被処理排水に凝集
剤を作用させてフロックを形成する反応槽と、側壁に配
置した電極の直上にフロック流入口を配置し、前記フロ
ック流入口を通じて供給された前記フロックを前記電極
から発生する電解ガス気泡と会合させて浮上させる浮上
槽と、前記フロックと被処理排水とを分離する分離槽と
、前記フロックを除去するスキーマ−とを備えた一次電
気浮上装置の後段に第二の浮上槽を設けた構成を備えて
いる。The electric flotation device, which is the basis of this application, includes a reaction tank that applies a flocculant to wastewater to be treated to form flocs, and a floc inlet placed directly above the electrodes placed on the side wall. A primary device comprising: a flotation tank that floats the supplied flocs by associating them with electrolytic gas bubbles generated from the electrodes; a separation tank that separates the flocs from wastewater to be treated; and a schema that removes the flocs. It has a configuration in which a second flotation tank is provided after the electric flotation device.
上記した手段によれば、−次電気浮上装置の電極を浮上
槽の側壁に配置し、その直上にフロック流入口を配置す
ることにより、浮上槽に流入したフロックを高密度の電
解ガス気泡と接触させることができるので、被処理排水
中のＳＳの殆どを一次電気浮上装置で除去することがで
きる。これにより、上記−次電気浮上装萱の後段に設け
た第二の浮上槽において、電解による酸化還元反応がＳ
Ｓによって阻害されることなく効率的に進行するので、
ＢＯＤ、ＣＯＤの殆どを除去することができ、有機排水
の高度処理を実現することができる。According to the above-mentioned means, the electrodes of the secondary electric levitation device are placed on the side wall of the flotation tank, and the floc inlet is placed directly above it, so that the flocs flowing into the flotation tank are brought into contact with high-density electrolytic gas bubbles. Therefore, most of the SS in the wastewater to be treated can be removed by the primary electric flotation device. As a result, the oxidation-reduction reaction due to electrolysis is carried out in the second flotation tank installed after the above-mentioned secondary electric flotation device.
Because it progresses efficiently without being inhibited by S,
Most of BOD and COD can be removed, and advanced treatment of organic wastewater can be realized.
以下、実施例により本発明を説明する。The present invention will be explained below with reference to Examples.
ご実施例〕
本実施例による電気浮上装置の要部の構成を第１図およ
び第２図に示す。Embodiment] FIGS. 1 and 2 show the configuration of the main parts of an electric levitation device according to this embodiment.
被処理有機排水は、スクリーンなどによって粗大ゴミを
取り除いた後、まず電気浮上装置１の一端に設けられた
排水流入口２を通じて第一の無機反応槽３ａに導入され
る。上記無機反応槽３ａ１＝は、有機排水の種類に応じ
て選択された、例えば塩化第二鉄などを含む無機凝集剤
が所定濃度注入されており、ここで排水のｐＨ調整が行
われるとともに、排水中の親水性物質の一部と凝集剤と
が作用してフロックが形成される。上記無機反応槽３ａ
には、排水を撹拌する撹拌手段４や、図示は省略するが
、排水のｐＨを測定するｐＨセンサなどが設置されてい
る。The organic wastewater to be treated is first introduced into the first inorganic reaction tank 3a through the wastewater inlet 2 provided at one end of the electric levitation device 1 after removing bulky waste using a screen or the like. The inorganic reaction tank 3a1= is injected with a predetermined concentration of an inorganic flocculant containing, for example, ferric chloride, which is selected according to the type of organic wastewater, and the pH of the wastewater is adjusted here. A part of the hydrophilic substance therein acts with the flocculant to form a floc. The above inorganic reaction tank 3a
A stirring means 4 for stirring the waste water, a pH sensor for measuring the pH of the waste water, etc. are installed, although not shown.
上記無機反応槽３ａの隣りには、同様の構成を備えた第
二の無機反応槽３ｂが設けられており、第一の無機反応
槽３ａで概ね調整された排水のｐＨｌ１７）微調整が行
われる。また、排水中の親水性物質の一部は、ここで凝
集してフロックを形成する。A second inorganic reaction tank 3b having a similar configuration is provided next to the inorganic reaction tank 3a, and the pH of the wastewater that has been roughly adjusted in the first inorganic reaction tank 3a is finely adjusted. . In addition, some of the hydrophilic substances in the wastewater aggregate here to form flocs.
上記第二の無機反応槽３ｂは、必要に応じて設けられる
もので、有機排水の種類によっては、第一の無機反応槽
３ａだけでよい場合もある。また、有機排水の種類によ
っては、第二の無機反応槽３ｂの後段に第三の無機反応
槽を設けてもよい。The second inorganic reaction tank 3b is provided as needed, and depending on the type of organic wastewater, only the first inorganic reaction tank 3a may be required. Further, depending on the type of organic wastewater, a third inorganic reaction tank may be provided after the second inorganic reaction tank 3b.
上記無機反応槽３ａ、３ｂて形成されたフロックは、排
水とともに隣りの高分子反応槽５に導入される。上記高
分子反応槽５には、有機排水の種類に応じて選択された
所定濃度の高分子凝集剤が注入されており、ここて上記
凝集剤と排水中の疎水性汚濁物質とが作用してフロック
が形成される。The flocs formed in the inorganic reaction tanks 3a and 3b are introduced into the adjacent polymer reaction tank 5 together with the waste water. A polymer flocculant at a predetermined concentration selected according to the type of organic wastewater is injected into the polymer reaction tank 5, and the flocculant and hydrophobic pollutants in the wastewater interact with each other. Flocks are formed.
なお、有機排水中の疎水性汚濁物質の濃度が高い場合は
、上記高分子反応槽５の後段に第二、またはさらに第三
の高分子反応槽を設置してもよい。Note that if the concentration of hydrophobic pollutants in the organic wastewater is high, a second or third polymer reaction tank may be installed after the polymer reaction tank 5.
上記無機反応槽３ａ、３ｂおよび高分子反応槽５で形成
されたフロックは、排水とともにフロック流入槽６を通
じて浮上槽７に導入される。上記フロック流入槽６には
、フロックを均一に浮上槽７に導入するだめの案内板８
が設けられている。The flocs formed in the inorganic reaction tanks 3a, 3b and the polymer reaction tank 5 are introduced into the flotation tank 7 through the floc inflow tank 6 together with the waste water. The floc inflow tank 6 has a guide plate 8 for uniformly introducing the flocs into the flotation tank 7.
is provided.
上記浮上槽７の下部側壁には、電極９が配置されている
。上記電極９は、複数の陽極と陰極とを交互に配置した
構造を有しており、水の電気分解によって陰極から発生
した水素ガス気泡が、陽極と陰極との隙間から浮上する
ようになっている。上記電極９の直上には、フロック流
入口１０が配置されており、フロックを含む排水は、上
記フロック流入口１０を通じて浮上槽７に導入される。Electrodes 9 are arranged on the lower side wall of the flotation tank 7. The electrode 9 has a structure in which a plurality of anodes and cathodes are arranged alternately, and hydrogen gas bubbles generated from the cathode by electrolysis of water float up from the gap between the anode and the cathode. There is. A floc inlet 10 is arranged directly above the electrode 9, and the waste water containing flocs is introduced into the flotation tank 7 through the floc inlet 10.
このように、上記浮上槽７は、その側壁に電極９を配置
し、上記電極９の直上にフロック流入口１０を配置した
構成になっているため、フロック流入口１０を通じて浮
上槽７に導入されたフロックは、電極９から発生する高
密度の水素ガス気泡と直ちに会合し、その浮力により浮
上槽７の側壁に沿って上昇する。またこのとき、電極９
の上方には、第２図に示すような対流（Ｂ）が形成され
るので、浮上槽７に導入された直後に水素ガス気泡と会
合できなかった少量のフロックも、この対流（Ｂ）に巻
き込まれて電極９の上方で再浮上し、水素ガス気泡と会
合して浮上する。なお、上記フロック流入口１０には、
逆流防止板１１が設けてあり、水素ガス気泡と会合して
浮上するフロックがフロック流入口１０を通じて流入口
６に逆流するのを防止している。In this way, the flotation tank 7 has the electrode 9 disposed on its side wall and the floc inlet 10 disposed directly above the electrode 9, so that the flocs are introduced into the flotation tank 7 through the floc inlet 10. The flocs immediately associate with high-density hydrogen gas bubbles generated from the electrode 9, and rise along the side wall of the flotation tank 7 due to their buoyancy. Also at this time, the electrode 9
Since a convection current (B) as shown in Fig. 2 is formed above, a small amount of flocs that were not able to associate with the hydrogen gas bubbles immediately after being introduced into the flotation tank 7 are also absorbed by this convection flow (B). It gets caught up and resurfaces above the electrode 9, and floats together with hydrogen gas bubbles. Note that the flock inlet 10 includes:
A backflow prevention plate 11 is provided to prevent flocs that float together with hydrogen gas bubbles from flowing back into the inlet 6 through the floc inlet 10.
上記電極９の側方および下方には、第２図に示すような
対流（Ａ）が形成される。排水はこの対流（Ａ）に沿っ
て電極９の隙間を下方から上方に流れ、電解による酸化
還元反応によって排水中のＢＯＤ、ＣＯＤ、色素などが
除去される。また、前述したように、浮上槽７に導入さ
れたフロックは、電極９上で水素ガス気泡と会合して浮
上するので、電極９の隙間を通過する排水中にはフロッ
クが殆ど含まれない。すなわち、上記浮上槽７は、フロ
ックによる電極９の隙間の目詰まりを防止することがで
きる構造となっている。Convection (A) as shown in FIG. 2 is formed on the sides and below the electrode 9. The wastewater flows from below to above through the gap between the electrodes 9 along this convection (A), and BOD, COD, pigments, etc. in the wastewater are removed by an oxidation-reduction reaction caused by electrolysis. Further, as described above, the flocs introduced into the flotation tank 7 combine with hydrogen gas bubbles on the electrodes 9 and float, so that the waste water passing through the gaps between the electrodes 9 contains almost no flocs. That is, the flotation tank 7 has a structure that can prevent the gaps between the electrodes 9 from being clogged with flocs.
一方、水素ガス気泡と会合して浮上したフロックは、排
水とともに分離！’！１２に導かれた後、その上方に設
けられたスキーマ−１３によって排水から分離され、汚
泥槽１４の排出口１４ａを通じて外部に排出される。水
素ガス気泡と会合して馬上したフロックは、高濃度の水
素ガス気泡を多タコ含むためにその浮力が大きく、従っ
て、−旦淳上したフロックが再沈澱することは殆どなし
）。このように、上記浮上槽７は、水素ガス気泡と会合
しないフロックが多量に発生ずるキアリオーバー現象を
確実に防止することができ、かつ−旦浮上したフロック
の再沈澱も防止することができる櫂造になってＬ′する
ので、排水中の５５．ＢＯＤ、ＣＯＤ、色素などを有効
に除去することができ、請にＳＳは、はぼ完全に除去す
る二とができる。また、上記浮上槽７におし）では、フ
ロック中に水沫ガス気泡が多量に含まれているので、ス
キーマ−１３によって排水かち分離されたフロック中の
含水率が少なく、これにより、汚泥槽１４の排出：１、
４ ａから排出されるスラッジの量を少なくすることが
できる。On the other hand, the flocs that float to the surface after combining with the hydrogen gas bubbles are separated along with the drainage! '! After being led to the sludge tank 12, the sludge is separated from the waste water by a schema 13 provided above, and is discharged to the outside through the discharge port 14a of the sludge tank 14. The flocs that float up in association with the hydrogen gas bubbles have a large buoyancy because they contain many high-concentration hydrogen gas bubbles; therefore, the flocs that have been lifted up are almost never re-sedimented. In this way, the flotation tank 7 is a paddle that can reliably prevent the chiariover phenomenon in which a large amount of flocs that do not combine with hydrogen gas bubbles is generated, and also prevent re-sedimentation of flocs that have already floated. Since the structure becomes L', 55. BOD, COD, pigments, etc. can be effectively removed, and SS can be almost completely removed. In addition, in the flotation tank 7), since the flocs contain a large amount of water droplet gas bubbles, the water content in the flocs drained and separated by the schema 13 is low. Emission: 1,
4. The amount of sludge discharged from a can be reduced.
上記のようにして、ＳＳがほぼ完全に除去された排水は
、−次処理水導管１５を通じて水位調議管】６に送られ
て水位の調整が行われた後、誘」管１７および処理水流
入槽１８を経て第二の浮上槽１９に導入される。上記水
位調整管１６と誘導管１７との間には、必要に応じて無
機反応槽３Ｃが設けられる。上記反応槽３Ｃには、排水
の種類に応じて選択された、例えば塩化第二鉄などを含
む無機凝集剤が所定濃度注入されており、ここで排水の
ｐＨの再調整が行われるとともに、排水中に僅かに残っ
ている親水性物質と凝集剤とが作用してフロックを形成
される。上記無機凝集剤は、電解によって次亜塩素ガス
や塩素ガスを発生するので、上記反応槽３Ｃを設けるこ
とにより、第二の浮上槽１９におけるＢＯＤ、ＣＯＤの
除去率および色素の脱色効果を向上させることができる
。As described above, the wastewater from which SS has been almost completely removed is sent to the water level adjustment pipe 6 through the next treated water conduit 15, and the water level is adjusted. The liquid is introduced into a second flotation tank 19 via an inflow tank 18 . An inorganic reaction tank 3C is provided between the water level adjustment pipe 16 and the guide pipe 17, if necessary. An inorganic flocculant containing, for example, ferric chloride is injected into the reaction tank 3C at a predetermined concentration, which is selected according to the type of wastewater, and the pH of the wastewater is readjusted here. A small amount of hydrophilic substance remaining inside and the flocculant interact to form flocs. Since the inorganic flocculant generates hypochlorite gas and chlorine gas through electrolysis, the provision of the reaction tank 3C improves the removal rate of BOD and COD and the decolorization effect of pigments in the second flotation tank 19. be able to.
なお、上記無機反応槽３Ｃには、前記無機反応槽３ａ、
３ｂと同様、排水を撹拌する撹拌手段４、排水のｐＨを
測定するｐＨセンサなどが設置されている。上記反応槽
３ＣでｐＨ調整された排水は、ポンプ２０によって誘導
管１７に送られ、次いで処理水流入槽１８に導入される
。Note that the inorganic reaction tank 3C includes the inorganic reaction tank 3a,
Similar to 3b, a stirring means 4 for stirring the waste water, a pH sensor for measuring the pH of the waste water, etc. are installed. The waste water whose pH has been adjusted in the reaction tank 3C is sent to the guide pipe 17 by the pump 20, and then introduced into the treated water inflow tank 18.
処理水流入槽１８に導入された上記排水は、その底部に
設けられた開口２１を通じて第二の浮上槽１９に導入さ
れる。上記浮上槽１９の底部側壁には、前記第一の浮上
Ｗ！７と同種の電極９が設けられている。排水は、この
電極９の隙間を下方から上方に流れ、電解による酸化還
元反応によってＢＯＤ、ＣＯＤ、色素などが除去される
。上記第二の浮上槽１９に導入された排水中の５５は、
その殆どが前記第一の浮上槽７て除去されているので、
上記酸化還元反応は、ＳＳによって阻害されることな（
効率的に進行する。これにより、前記第一の浮上槽７で
除去できなかった残りのＢＯＤＣＯＤ、色素などは、上
記第二の浮上槽１９てほぼ完全に除去される。一方、電
極９から発生する水素ガス気泡と会合して浮上した少量
のフロックは、排水とともに分ｎ横２２に導かれた後、
その上方に設けられたスキーマ−１３によって排水から
分離され、汚泥槽１４の排出口１４ａを通じて外部に排
出される。また、分離槽２２に導入された排水は、二次
処理水導管２３を経て水位調整管１６に送られ、必要に
応じてｐＨ調整などが付われた後、外部に排出される。The wastewater introduced into the treated water inflow tank 18 is introduced into the second flotation tank 19 through an opening 21 provided at the bottom thereof. On the bottom side wall of the flotation tank 19, the first flotation W! An electrode 9 of the same type as 7 is provided. The waste water flows from below to above through the gap between the electrodes 9, and BOD, COD, pigments, etc. are removed by an oxidation-reduction reaction caused by electrolysis. 55 in the waste water introduced into the second flotation tank 19,
Since most of it has been removed by the first flotation tank 7,
The above redox reaction is not inhibited by SS (
Proceed efficiently. As a result, the remaining BODCOD, pigment, etc. that could not be removed in the first flotation tank 7 are almost completely removed in the second flotation tank 19. On the other hand, a small amount of flocs that floated together with the hydrogen gas bubbles generated from the electrode 9 were led to the horizontal direction 22 along with the drainage water.
It is separated from the waste water by a schema 13 provided above, and is discharged to the outside through the discharge port 14a of the sludge tank 14. Further, the wastewater introduced into the separation tank 22 is sent to the water level adjustment pipe 16 via the secondary treated water conduit 23, and after being subjected to pH adjustment as necessary, is discharged to the outside.
このように、本実施例の電気浮上装置１によれば、第一
の浮上槽７で排水中のＳＳをほぼ完全に除去することが
でき、第二の浮上槽１９で排水中のＢＯＤ、ＣＯＤ、色
素などをほぼ完全に除去することができるので、従来の
生物的処理装置と同等、もしくはそれ以上の高度有機排
水処理を、生物的処理装置に比べて少ない設置面積、施
設費、ランニングコストで実現することができる。ちな
みに、上記電気浮上装置１は、同等の処理能力を有する
従来の生物的処理装置に比べて、排水処理施設面積で１
１５〜１／１０、施設費で５０〜７０％、ランニングコ
ストで５０〜７０％の低減を実現できる二とが、本発明
者の実験により判明し上記電気浮上装置１を用ヒ）で実
施した有機排水（水産加工排水）処理の分析値の一例を
下記の表に示す。As described above, according to the electric flotation device 1 of this embodiment, the SS in the drain water can be almost completely removed in the first flotation tank 7, and the BOD and COD in the drain water can be removed in the second flotation tank 19. Since it is possible to almost completely remove pigments, etc., it is possible to perform advanced organic wastewater treatment equivalent to or better than conventional biological treatment equipment, with less installation space, facility costs, and running costs compared to biological treatment equipment. It can be realized. By the way, the above-mentioned electric levitation device 1 has a wastewater treatment facility area of 1 less than a conventional biological treatment device with the same treatment capacity.
The present inventor's experiments revealed that the above electric levitation device 1 can be used in the following manner. An example of analysis values for organic wastewater (fisheries processing wastewater) treatment is shown in the table below.
表中、被処理排水は、解凍、洗浄および解体加工後の水
産加工排水を用いた（排水量：１００ｍ’７日）。In the table, as the wastewater to be treated, fishery processing wastewater after thawing, washing, and disassembly processing was used (discharge volume: 100 m'7 days).
被処理排水は、集水槽にて粗大ゴミの除去、油水分離槽
にて浮上分離、ストレーナによる微細ゴミの除去後、流
量調整槽に送り、腐敗防止のため曝気したもので、採取
点は電気浮上装置の入口で行った。The wastewater to be treated is treated by removing bulky debris in a water collection tank, flotation separation in an oil-water separation tank, and removing fine debris by a strainer, and then sent to a flow rate adjustment tank where it is aerated to prevent spoilage.The collection point is electrically floated. This was done at the entrance of the device.
表
以上、本発明を実施例により説明したが、本発明は上記
実施例に限定されるものではなく、その要旨を変更しな
い範囲で種々の設計変更を行うことができる。Although the present invention has been explained using Examples above, the present invention is not limited to the above-mentioned Examples, and various design changes can be made without changing the gist thereof.
本願において開示される発明のうち、代表的なものによ
って得ちれる効果を簡単に説明すれば、次のとおりであ
る。Among the inventions disclosed in this application, the effects obtained by typical inventions are briefly explained below.
（ｊ）、従来の生物的処理装置に比べて、処理施設の面
積を大幅に縮小することができる。(j) Compared to conventional biological treatment equipment, the area of the treatment facility can be significantly reduced.
（２）、従来の生物的処理装置に比べて、施設費を大巾
晶ｊこ削減することができる。(2) Compared to conventional biological treatment equipment, facility costs can be significantly reduced.
（３）、従来の生物的処理装置に比べて、ランニングコ
ストを大幅に削減することができる。特に、生物的処理
装置と異−；す、曝気槽を必要と巳な１．）ので、消費
電力を大幅に削減することができる。(3) Running costs can be significantly reduced compared to conventional biological treatment equipment. In particular, unlike biological treatment equipment, an aeration tank is required. ), power consumption can be significantly reduced.
（４） 水産加工排水などに含まれる蛋白質の再利用
が可能となる。(4) It becomes possible to reuse proteins contained in wastewater from seafood processing.
（５）、濾過法によらないで、ＳＳを完全除去すること
ができる。(5) SS can be completely removed without using a filtration method.
（６）、ＢＯＤ２０ ｐｐｍ以下、ｃｏＤ３ｏｐｐｍ以
下の高度処理を実現することができるので、被処理排水
の再利用が可能となる。(6) Since it is possible to achieve advanced treatment with BOD of 20 ppm or less and coD of 3 oppm or less, it is possible to reuse the wastewater to be treated.
第１図は、本発明の一実施例である電気浮上装置の全体
構成を示す概略図、
第２図は、この電気浮上装置の要部断面図である。
１・・・電気浮上装置、２・・・排水流入口、３ａ、３
ｂ、３ｃ・・・無機反応槽、４・・・撹拌手段、５・・
・高分子反応槽、６・・・フロック流入口、７．１９・
・・浮上槽、８・・・案内板、９・・・電極、１０・・
・フロック流入口、１１・・・逆流防止板、１２．２２
・・・分離槽１３・・・スキーマ−１４・・・汚泥槽、
１４ａ・・・汚泥排出口、】５・・・−次処理水導管１
６・・・水位調整管、１７・・・誘導管、１８・・・処
理水流入口、２０・・・ポンプ、２１・・・開口、２３
・・・二次処理水導管。
特許出願人 システム ゲイト株式会社同
株式会社 タ フ 開 発代理人 弁理士 筒 井
大 相FIG. 1 is a schematic diagram showing the overall configuration of an electric levitation device according to an embodiment of the present invention, and FIG. 2 is a sectional view of a main part of this electric levitation device. 1...Electric levitation device, 2...Drainage inlet, 3a, 3
b, 3c... Inorganic reaction tank, 4... Stirring means, 5...
・Polymer reaction tank, 6...floc inlet, 7.19・
...Flotation tank, 8...Guide plate, 9...Electrode, 10...
・Flock inlet, 11... Backflow prevention plate, 12.22
...Separation tank 13...Schema-14...Sludge tank,
14a...Sludge discharge port, ]5...-Next treated water conduit 1
6... Water level adjustment pipe, 17... Guide pipe, 18... Treated water inlet, 20... Pump, 21... Opening, 23
...Secondary treated water conduit. Patent applicant System Gate Co., Ltd.
Tahu Co., Ltd. Development Agent Patent Attorney Tsutsui
Grand phase
Claims (1)
る反応槽と、側壁に配置した電極の直上にフロック流入
口を配置し、前記フロック流入口を通じて供給される前
記フロックを前記電極から発生する電解ガス気泡と会合
させて浮上させる浮上槽と、前記フロックと被処理排水
とを分離する分離槽と、前記フロックを除去するスキー
マーとを備えた電気浮上装置の後段に第二の浮上槽を設
けたことを特徴とする電気浮上装置。 ２、前記第二の浮上槽の前段に、被処理排水のｐＨを微
調整するための反応槽を設けたことを特徴とする請求項
１記載の電気浮上装置。[Scope of Claims] 1. A reaction tank in which a flocculant is applied to wastewater to be treated to form flocs, and a floc inlet is disposed directly above an electrode disposed on a side wall, and the floc is supplied through the floc inlet. A downstream part of an electric flotation device comprising a flotation tank that causes flocs to float by associating them with electrolytic gas bubbles generated from the electrodes, a separation tank that separates the flocs from wastewater to be treated, and a schemer that removes the flocs. An electric levitation device characterized in that a second levitation tank is provided. 2. The electric flotation device according to claim 1, further comprising a reaction tank for finely adjusting the pH of the wastewater to be treated, provided upstream of the second flotation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24969290A JPH04131185A (en) | 1990-09-19 | 1990-09-19 | Electric floating device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP24969290A JPH04131185A (en) | 1990-09-19 | 1990-09-19 | Electric floating device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH04131185A true JPH04131185A (en) | 1992-05-01 |
Family
ID=17196785
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP24969290A Pending JPH04131185A (en) | 1990-09-19 | 1990-09-19 | Electric floating device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH04131185A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100355955B1 (en) * | 2000-01-24 | 2002-10-12 | 한무영 | Apparatus for Generating Microbubbles with Positive Charge by Electrolysis |
| KR20020094706A (en) * | 2001-06-13 | 2002-12-18 | 한무영 | Removal method of organic suspension material from livestock wastewater by electroflotation |
| JP2007319817A (en) * | 2006-06-02 | 2007-12-13 | Yanmar Co Ltd | Wastewater treatment method and its equipment, and wastewater treatment apparatus |
| WO2010092265A1 (en) * | 2009-02-16 | 2010-08-19 | Orege | Method and device for scrubbing effluents |
| WO2013156002A1 (en) * | 2012-04-19 | 2013-10-24 | 波鹰(厦门)科技有限公司 | Nano catalyst electrolysis flocculation air flotation device |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52146964A (en) * | 1976-06-01 | 1977-12-07 | Mitsubishi Electric Corp | Process for treating waste waters drained from fisheries working |
-
1990
- 1990-09-19 JP JP24969290A patent/JPH04131185A/en active Pending
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS52146964A (en) * | 1976-06-01 | 1977-12-07 | Mitsubishi Electric Corp | Process for treating waste waters drained from fisheries working |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100355955B1 (en) * | 2000-01-24 | 2002-10-12 | 한무영 | Apparatus for Generating Microbubbles with Positive Charge by Electrolysis |
| KR20020094706A (en) * | 2001-06-13 | 2002-12-18 | 한무영 | Removal method of organic suspension material from livestock wastewater by electroflotation |
| JP2007319817A (en) * | 2006-06-02 | 2007-12-13 | Yanmar Co Ltd | Wastewater treatment method and its equipment, and wastewater treatment apparatus |
| WO2010092265A1 (en) * | 2009-02-16 | 2010-08-19 | Orege | Method and device for scrubbing effluents |
| CN102438955A (en) * | 2009-02-16 | 2012-05-02 | 奥里格公司 | Method and device for scrubbing effluents |
| WO2013156002A1 (en) * | 2012-04-19 | 2013-10-24 | 波鹰(厦门)科技有限公司 | Nano catalyst electrolysis flocculation air flotation device |
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