JPH0688018B2 - Flotation device - Google Patents
Flotation deviceInfo
- Publication number
- JPH0688018B2 JPH0688018B2 JP1310539A JP31053989A JPH0688018B2 JP H0688018 B2 JPH0688018 B2 JP H0688018B2 JP 1310539 A JP1310539 A JP 1310539A JP 31053989 A JP31053989 A JP 31053989A JP H0688018 B2 JPH0688018 B2 JP H0688018B2
- Authority
- JP
- Japan
- Prior art keywords
- pipe
- water supply
- tube
- raw water
- tank
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired - Fee Related
Links
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Physical Water Treatments (AREA)
Description
【発明の詳細な説明】 〔産業上の利用分野〕 本発明は浮上分離装置に関し、詳しくは水処理における
浮遊懸濁粒子や油等の分離のために用いる浮上分離装置
に関する。Description: TECHNICAL FIELD The present invention relates to a flotation device, and more particularly to a flotation device used for separating suspended particles and oil in water treatment.
加圧浮上分離法は、水処理における浮遊懸濁粒子や油の
分離のほか浮遊選鉱法等に利用されている。この加圧浮
上分離法は、気体は極めて密度が小さいために、該気体
の微細気泡を作り、これを浮遊懸濁粒子や油滴の界面に
付着させると、浮遊懸濁粒子や油滴の見かけの比重が小
さくなり、液体との密度差により浮上する現象を利用し
た技術である。The pressurized flotation method is used for floating flotation method as well as separation of suspended suspended particles and oil in water treatment. In this pressurized flotation method, the gas has a very low density, so if you create fine bubbles of the gas and attach them to the interface of suspended suspended particles or oil droplets, you can see the suspended suspended particles or oil droplets. This is a technology that utilizes the phenomenon that the specific gravity of the water becomes smaller and the material floats due to the difference in density with the liquid.
一般に用いられている加圧浮上分離装置は、流入原水ま
たは処理水の一部を十分な空気の存在下で加圧し、空気
がほとんど飽和状態になるまで溶解させる方式のもので
ある。この際の圧力は、通常２〜5kg/cm2Gである。この
加圧水を浮上分離装置の中で大気圧中に開放すると、多
数の微細な気泡が放出され、放出された気泡は原水中の
浮遊懸濁粒子や油滴の界面に付着して浮上する。浮遊懸
濁粒子や油滴が微細な場合は、さらに凝集剤を注入して
フロックを形成させた後、前述の微細気泡をこのフロッ
クに付着させて浮上せしめる。このようにして浮上させ
た浮遊懸濁粒子や油滴を集め、系外に除去することによ
り良好な清澄水を得ることができる。従来型の加圧浮上
分離法のうち、処理水の一部を循環させ、この循環水を
浮上分離装置に戻す方法のブロックフローを第１図に示
す。The pressure-floating separation device generally used is a system of pressurizing a part of inflowing raw water or treated water in the presence of sufficient air to dissolve the air until it is almost saturated. The pressure at this time is usually 2 to 5 kg / cm 2 G. When this pressurized water is released to atmospheric pressure in the flotation device, a large number of fine bubbles are released, and the released bubbles adhere to the surface of suspended suspended particles and oil droplets in the raw water and float up. When the suspended particles or oil droplets are fine, a flocculant is further injected to form flocs, and then the fine bubbles described above are adhered to the flocs and floated. By collecting the floating suspended particles and oil droplets thus floated and removing them outside the system, good clear water can be obtained. FIG. 1 shows a block flow of a method of circulating a part of the treated water and returning the circulated water to the levitation separation apparatus in the conventional pressurized levitation separation method.
加圧浮上分離法は沈澱法と比較すると、処理時間が短
く、しかも装置をコンパクトにできると言われている
が、それはそれぞれの装置の沈澱槽と浮上槽における滞
留時間や大きさのみを比較した場合であって、加圧浮上
分離装置には実際上、懸濁粒子や油滴の凝集に要する凝
集槽，加圧水を作る加圧槽が必要である。これら装置に
おける所要時間を考慮すると、下表の如く、両者の処理
時間は大差がない。The pressure levitation separation method is said to be shorter in processing time than the precipitation method, and it is said that the equipment can be made compact, but only the residence time and size in the precipitation tank and flotation tank of each device were compared. In some cases, the pressure flotation device actually requires a flocculation tank required for flocculation of suspended particles and oil droplets, and a pressure tank for producing pressurized water. Considering the time required for these devices, there is no great difference in the processing time between the two, as shown in the table below.
従って、水処理において加圧浮上分離法を採用して従来
よりも高性能なものにするためには、より効率の高い凝
集法，浮上法，加圧法を考えなければならない。 Therefore, in order to adopt the pressure flotation separation method in water treatment to achieve higher performance than the conventional method, it is necessary to consider a more efficient flocculation method, flotation method, or pressure method.
すなわち、本発明は底部中央に立設した原水供給ノズル
と循環水供給ノズルより流入する液を混ぜる混合部〔こ
の混合部は、本発明の装置が円筒型の場合は、ドラフト
チューブや仕切り板による部分であり、装置が矩型の場
合は、仕切り板による部分である（以下、ドラフトチュ
ーブを代表として示す。）〕を有し、上部にスカム掻き
取り機とスカム排出口を設け、下部に処理水排出口を設
けた浮上分離槽、内径の小さい第１のチューブと該チュ
ーブと接続する内径の大きい第２のチューブからなり、
気体の不在下にてフロックを形成せしめるループ状フロ
ック形成管であって、前記ドラフトチューブ内と連通し
ており、かつ該ドラフトチューブ内の先端部に上向きの
ノズルを取り付けたフロック形成管、該フロック形成管
と接続する原水供給管、該原水供給管と接続する凝集剤
供給手段、前記処理水排出口と接続しており、処理水抜
出し口と循環用処理水供給口を有する処理水槽、該循環
用処理水供給口と前記ドラフトチューブ内と連通し、か
つ該ドラフトチューブ内の前記上向きのノズルの直下に
下向きに設けた循環水供給ノズルとを接続する配管、該
配管の中間部に設けた互に連通する複数本のＵ字型加圧
管、該Ｕ字型加圧管の上流側配管と接続する空気供給手
段、該Ｕ字型加圧管の下流側に位置し、該Ｕ字型加圧管
および前記配管と接続する気液分離槽、該気液分離槽上
部に設けた空気抜き弁、該気液分離槽の下流側配管に設
けた減圧弁を備えていることを特徴とする浮上分離装置
を提供するものである。That is, the present invention is a mixing section that mixes the liquids flowing in from the raw water supply nozzle and the circulating water supply nozzle that are erected in the center of the bottom (this mixing section is a draft tube or a partition plate when the apparatus of the present invention is a cylindrical type). If the device is a rectangular type, it is a part by a partition plate (hereinafter, a draft tube is representatively shown)], and a scum scraping machine and a scum discharge port are provided in the upper part, and the processing is performed in the lower part. A flotation separation tank provided with a water discharge port, a first tube having a small inner diameter and a second tube having a large inner diameter connected to the tube,
A loop-shaped flock forming tube for forming flock in the absence of gas, the flock forming tube communicating with the inside of the draft tube, and having an upward nozzle attached to the tip of the draft tube, A raw water supply pipe connected to the forming pipe, a coagulant supply means connected to the raw water supply pipe, a treated water tank connected to the treated water discharge port and having a treated water outlet and a treated water supply port for circulation, the circulation For connecting the treated water supply port with the inside of the draft tube and for connecting the circulating water supply nozzle provided downward just below the upward nozzle in the draft tube, and a pipe provided at an intermediate portion of the pipe. A plurality of U-shaped pressurizing pipes, an air supply means connected to an upstream pipe of the U-shaped pressurizing pipe, a U-shaped pressurizing pipe located on the downstream side of the U-shaped pressurizing pipe and the above-mentioned Plumbing and A levitation separation device comprising: a continuous gas-liquid separation tank, an air vent valve provided at an upper portion of the gas-liquid separation tank, and a pressure reducing valve provided at a downstream side pipe of the gas-liquid separation tank. is there.
加圧水を効率よく製造するためには、水に流入する空気
の溶解効率を高くすると共に、浮上分離槽における気泡
の滞留時間を短縮させなければならない。ところで、空
気の溶解効率は、下記の式で表わすことができる。In order to efficiently produce pressurized water, it is necessary to increase the dissolution efficiency of air flowing into water and shorten the residence time of bubbles in the flotation tank. By the way, the dissolution efficiency of air can be expressed by the following formula.
ここで、η＝空気溶解効率 （％） Qi＝導入空気量 （Ｎ/hr） Qe＝余剰排出空気量（Ｎ/hr） Qd＝理論空気溶解量（Ｎ/hr） （ヘンリーの法則に従う） 従来法の加圧槽にコンプレッサーにより空気を供給した
場合のηは30〜60％であり、浮上分離槽におけるその滞
留時間は数分〜10数分である。これに対し、本発明によ
る高効率加圧水製造法においては、加圧ポンプの吸引側
より空気を吸引してもよく、またはコンプレッサーを使
用してもよいが、加圧槽を使用せずにＵ字型加圧管中に
て循環水中に空気を溶解させる。この方法によれば、従
来循環水は加圧槽で13分の滞留時間を要してη＝50％を
得ていたのに対し、同じη値を得るのに、わずか45秒の
滞留時間にて行うことができる。また、加圧水は加圧管
を通過後、気液分離槽に導かれて余剰空気は分離され
る。この気液分離槽における循環水の滞留時間は１分以
内である。 Where η = air dissolution efficiency (%) Qi = introduced air amount (N / hr) Qe = excess discharge air amount (N / hr) Qd = theoretical air dissolution amount (N / hr) (following Henry's law) When air is supplied to the pressure tank of the method by a compressor, η is 30 to 60%, and its residence time in the flotation tank is several minutes to several tens of minutes. On the other hand, in the high-efficiency pressurized water production method according to the present invention, air may be sucked from the suction side of the pressure pump or a compressor may be used, but a U-shape is used without using a pressure tank. Dissolve air in circulating water in a mold pressurizing tube. According to this method, η = 50% was obtained for the circulating water in the conventional pressurization tank, which required a residence time of 13 minutes, whereas the same η value was obtained with a residence time of only 45 seconds. Can be done by Further, the pressurized water, after passing through the pressurizing pipe, is guided to the gas-liquid separation tank to separate excess air. The residence time of the circulating water in this gas-liquid separation tank is within 1 minute.
次に、浮遊懸濁物や油分の除去率を考えると、浮上分離
槽における原水流入ノズルおよび加圧循環水流入ノズル
の位置関係は重要な因子である。従来の装置における両
ノズルの位置は、浮上分離装置内に設けられたドラフト
チューブ等の部分に同方向，同位置，接線方向等である
が、本発明者らは両ノズルを同位置に設けると共に、原
水流入側を上向き、加圧水流入側を下向きとなるように
すると、浮遊懸濁物や油分の除去率が高くなることを見
出した。Next, considering the removal rate of suspended solids and oil, the positional relationship between the raw water inflow nozzle and the pressurized circulating water inflow nozzle in the flotation separation tank is an important factor. The positions of both nozzles in the conventional device are the same direction, the same position, the tangential direction, etc. in the portion such as the draft tube provided in the levitation separation device. It was found that when the raw water inflow side is facing upward and the pressurized water inflow side is facing down, the removal rate of suspended solids and oil is high.
一方、凝集剤添加により微細な浮遊懸濁物や油滴を凝集
させて除去する方法は、凝集沈澱法等において従来から
行なわれている方法である。その一般的方法は、原水に
凝集剤を添加したのち、急速撹拌が１〜５分間なされ、
次いでフロック成長のために緩速撹拌が20〜40分間なさ
れた後、強固になったフロックを沈澱槽に導くものであ
る。これに対し、本発明者らは撹拌槽、撹拌機を使用せ
ず、かつ気体の不在下で極めて短時間で急速および緩速
撹拌する方法として、ループ状のチューブを使用するこ
とが有効であることを見出した。すなわち該チューブに
原水を流し、そのチューブ内に凝集剤を添加する方法で
ある。この方法によれば、急速撹拌は約10秒，緩速撹拌
は約１分という短時間で微細な浮遊懸濁物や油滴を十分
に凝集させることができる。原水中の浮遊懸濁物や油分
などを配管内にて凝集させる方法として、上下にＵター
ンさせる方法が既に実施されている。しかし、チューブ
をループ状に巻き、この中に原水と凝集剤を通過させて
優れたフロックを短時間に形成させる方法は未だ報告さ
れていない。本発明においてループ状フロック形成管
は、好ましくは内径の小さい第１のチューブと該チュー
ブに接続する内径の大きい第２のチューブよりなるもの
を用い、急速撹拌および緩速撹拌を行う。この撹拌の条
件は下記に示す通りで 急速撹拌 Ｇ＝1,500〜2,00/sec. Ｔ＝５〜15sec. 緩速撹拌 Ｇ＝100〜300/sec. Ｔ＝60sec. ここで、Ｇ＝速度勾配 （1/sec.） Ｔ＝滞留時間 （sec.） Re＝レイノルズ数 Ｄ＝管 径 （ｍ） ρ＝流体の密度 （kg/m3） ΔＰ＝圧力損失 （kg・w/m2） Ｌ＝管 長 （ｍ） ｇ＝重力換算係数（9.8kg・m/kg・ｗ・sec2） 本発明の加圧浮上分離装置は、上述した特徴を有する従
来の加圧浮上分離装置とは異なったものであり、その１
例を第２図により説明する。On the other hand, a method of flocculating and removing fine floating suspensions and oil droplets by adding a flocculating agent is a method that has been conventionally used in the flocculation and precipitation method and the like. The general method is that after adding the flocculant to the raw water, rapid stirring is performed for 1 to 5 minutes,
Then, after slow stirring for 20 to 40 minutes for floc growth, the hardened flocs are introduced into the precipitation tank. On the other hand, the present inventors are effective in using a loop-shaped tube as a method of rapidly and slowly stirring in an extremely short time in the absence of gas without using a stirring tank and a stirrer. I found that. That is, it is a method of flowing raw water into the tube and adding a coagulant into the tube. According to this method, fine floating suspensions and oil droplets can be sufficiently aggregated in a short time of about 10 seconds for rapid stirring and about 1 minute for slow stirring. A method of making a U-turn up and down has already been carried out as a method of aggregating floating suspensions and oil components in raw water in a pipe. However, a method of winding a tube in a loop shape and passing raw water and a coagulant through the tube to form an excellent floc in a short time has not yet been reported. In the present invention, the loop-shaped flock forming tube preferably comprises a first tube having a small inner diameter and a second tube having a large inner diameter connected to the tube, and performs rapid stirring and slow stirring. The conditions of this agitation are as follows: rapid agitation G = 1,500 to 2,000 / sec. T = 5 to 15 sec. Slow agitation G = 100 to 300 / sec. T = 60 sec. Where G = speed gradient (1 / sec.) T = residence time (sec.) Re = Reynolds number D = Pipe diameter (m) ρ = Fluid density (kg / m 3 ) ΔP = Pressure loss (kg ・ w / m 2 ) L = Pipe length (m) g = Gravity conversion factor (9.8kg ・m / kg · w · sec 2 ) The pressure levitation separation device of the present invention is different from the conventional pressure levitation separation device having the above-mentioned characteristics.
An example will be described with reference to FIG.
浮遊懸濁物や油分を含有する原水１は原水供給ポンプ２
を通り配管を流れ、凝集剤槽３より凝集剤供給ポンプ４
を通ってきた凝集剤と混合したのち、ループ状フロック
形成管５に導入される。ループ状フロック形成管５の断
面は、通常円形であるが、楕円形や四隅にＲをとった四
角形でもよい。また、ループ状フロック形成管５は、単
独で組み立ててもよいが、浮上分離槽６の周囲に巻きつ
けてもよい。さらに、ループ状フロック形成管５は、２
種類の異なる内径を有するチューブで形成する。急速撹
拌を行う第１のチューブの内径は小さく、速度勾配Ｇ値
を1,500〜2,000sec.-1とし、滞留時間Ｔを５〜15sec.と
する。続いて、緩速撹拌を行う内径の大きい第２のチュ
ーブに接続する。この第２のチューブ内の速度勾配Ｇ値
を100〜300sec.-1とし、滞留時間Ｔを約60sec.とする。
ここで、急速撹拌の速度勾配Ｇ値が1,500sec.-1未満で
あると、混合が不十分であり、2,000sec.-1を超える撹
拌は、経済性の点で問題がある。また、緩速撹拌の速度
勾配Ｇ値が100sec.-1未満であると、フロックの形成が
不十分となり、300sec.-1を超えると、逆に生成したフ
ロックが破壊されてしまう。Raw water 1 containing floating suspension and oil is a raw water supply pump 2
Flow through the pipe through the coagulant tank 3 and the coagulant supply pump 4
After mixing with the coagulant that has passed through, it is introduced into the loop-shaped flock forming tube 5. The cross section of the loop-shaped flock forming tube 5 is usually circular, but may be elliptical or quadrangular with R at four corners. The loop-shaped flock forming tube 5 may be assembled independently, but may be wound around the floating separation tank 6. Furthermore, the loop-shaped flock forming tube 5 has two
It is made of tubes with different inner diameters. The inner diameter of the first tube for rapid stirring is small, the velocity gradient G value is 1,500 to 2,000 sec.- 1 , and the residence time T is 5 to 15 sec. Then, it is connected to a second tube having a large inner diameter for performing slow stirring. The velocity gradient G value in the second tube is set to 100 to 300 sec.- 1 , and the residence time T is set to about 60 sec.
Here, when the velocity gradient G value of the rapid stirring is less than 1,500 sec. -1 , the mixing is insufficient, and stirring exceeding 2,000 sec. -1 has a problem in economical efficiency. Further, velocity gradient G value of slow agitation is less than 100 sec. -1, formation of flocs is insufficient, 300 sec. Exceeds -1, flocs produced in the opposite is destroyed.
ループ状フロック形成管５を出た原水は、次いで浮上分
離槽本体６にあるドラフトチューブ８内の原水供給ノズ
ル10を通り、浮上分離槽本体６に供給される。この原水
供給ノズル10は、水平に入ってきた管を上向きにしてい
ること並びに循環水供給ノズル23より上方に位置せしめ
たことに特徴がある。原水供給ノズル10の先端と循環水
供給ノズル23の先端の距離は、ノズルの外径によるベン
ド（90゜）により決定されるが、できるだけ短かくする
ことが望ましく、通常は30〜300mm程度とすべきであ
る。The raw water that has exited the loop-shaped flock forming tube 5 then passes through the raw water supply nozzle 10 in the draft tube 8 in the flotation separation tank body 6 and is supplied to the flotation separation tank body 6. The raw water supply nozzle 10 is characterized in that the pipe that has entered horizontally is directed upward and that it is positioned above the circulating water supply nozzle 23. The distance between the tip of the raw water supply nozzle 10 and the tip of the circulating water supply nozzle 23 is determined by the bend (90 °) depending on the outer diameter of the nozzle, but it is desirable to make it as short as possible, usually about 30 to 300 mm. Should be.
ドラフトチューブ８内には微小気泡と凝集フロックが混
在し、気泡の付着した凝集フロックは浮上分離槽本体６
の上方へ浮上する。浮上分離槽本体６における原水と循
環水の上昇速度は、通常10〜30m/hrである。凝集フロッ
クは上昇した後、浮上分離槽本体６の表面にて回転スカ
ム掻き取り機７により掻き取られ、スカム９として槽外
へ排出される。Micro-bubbles and flocs of flocculation are mixed in the draft tube 8, and flocs of flocculation with bubbles adhere to the floating separation tank body 6
Surface above. The rising speed of raw water and circulating water in the flotation tank body 6 is usually 10 to 30 m / hr. After the flocculation flocs rise, they are scraped off by the rotating scum scraper 7 on the surface of the flotation tank main body 6, and discharged as scum 9 out of the tank.
処理水排出口11は、浮上分離槽本体６の下部に設けられ
ており、処理水はここを通り処理水槽12に入り、処理水
13として系外へ排出されるが、一部は循環水14として使
用される。循環水量は、原水量の20〜60％程度が適当で
ある。The treated water discharge port 11 is provided in the lower part of the flotation / separation tank main body 6, and the treated water passes through here and enters the treated water tank 12 to be treated water.
It is discharged outside the system as 13, but part of it is used as circulating water 14. 20-60% of the amount of circulating water is suitable for the amount of circulating water.
循環水14の目的は、ガス（通常は空気）を加圧し溶解せ
しめ、浮上分離槽本体６に入る前に減圧して溶解したガ
スを微小気泡として取り出すことである。加圧の方法と
しては、加圧ポンプ16の吸引側より空気15を吸引する方
法がとられるが、大規模装置の場合はコンプレッサー17
を使用して、加圧ポンプ吐出側に空気を供給してもよ
い。導入する空気量は、通常空気量／循環水量＝0.1で
あり、圧力は5kg/cm2・Ｇを標準とする。加圧された循
環水14は、Ｕ字型加圧管18に導入され、配管内を上下に
移動しながら通過する間に気泡が効率よく水に溶解す
る。管内流速は0.2m/sec.以上とすべきである。これ以
下の流速では効率のよい空気の溶解が行われない。ま
た、管内の滞留時間は45〜90sec.で十分であり、これは
通常の加圧槽の滞留時間１〜５分と比べ大巾に短縮する
ことができる。加圧された循環水は、気液分離槽19に導
入され、余剰空気は空気抜き弁20より系外に排出され
る。余剰空気が無くなった加圧循環水21は、減圧弁22を
通り循環水供給ノズル23に導かれる。The purpose of the circulating water 14 is to pressurize and dissolve a gas (usually air), and decompress it before entering the floating separation tank main body 6 to take out the dissolved gas as fine bubbles. As a method of pressurizing, a method of sucking the air 15 from the suction side of the pressurizing pump 16 is used, but in the case of a large-scale device, a compressor 17
May be used to supply air to the discharge side of the pressure pump. The amount of air to be introduced is usually air amount / circulating water amount = 0.1, and the standard pressure is 5 kg / cm 2 · G. The pressurized circulating water 14 is introduced into the U-shaped pressurizing pipe 18, and bubbles are efficiently dissolved in the water while passing through the pipe while moving up and down. The flow velocity in the pipe should be 0.2 m / sec. Or more. At a flow velocity lower than this, efficient air dissolution is not performed. Further, the residence time in the pipe is sufficient to be 45 to 90 seconds, which can be greatly shortened as compared with the residence time in an ordinary pressure tank of 1 to 5 minutes. The pressurized circulating water is introduced into the gas-liquid separation tank 19, and the surplus air is discharged from the system through the air vent valve 20. The pressurized circulating water 21 from which the excess air has been removed is guided to the circulating water supply nozzle 23 through the pressure reducing valve 22.
循環水供給ノズル23は、ドラフトチューブ８内に水平に
入ってきた管を上向きにしていること並びに原水供給ノ
ズル10の直下に位置せしめたことに特徴がある。減圧弁
22を通過後、循環水は常圧に戻り、溶解していた空気は
微小気泡となる。The circulating water supply nozzle 23 is characterized in that the pipe that has entered horizontally in the draft tube 8 is directed upward and that it is located directly below the raw water supply nozzle 10. Pressure reducing valve
After passing through 22, the circulating water returns to normal pressure, and the dissolved air becomes fine bubbles.
以上、本発明の加圧浮上分離装置とその使用法について
述べたが、本発明の装置と従来の装置を比較して以下に
要約する。The pressure levitation separation apparatus of the present invention and the method of using the same have been described above. The apparatus of the present invention and the conventional apparatus will be compared and summarized below.
従来の浮上分離装置を用いた場合、浮遊懸濁物や油分の
凝集を行うため、急速撹拌に１〜５分、緩速撹拌に20〜
40分要していたが、本発明ではループ状フロック形成管
を採用したことにより、急速撹拌は５〜15sec.、緩速撹
拌では約60sec.でよく、大巾な短縮が可能である。ま
た、浮上分離槽における浮上速度は、従来法では５〜8m
/hrであったものが、本発明によれば10〜30m/hrとな
り、浮上分離槽のコンパクト化を促進することができ
る。さらに、循環水の加圧滞留時間は従来法の１〜５分
に比較して45〜90sec.となり、大巾に滞留時間を短縮で
きる。When a conventional flotation device is used, flocculation of suspended suspension and oil is performed, so 1-5 minutes for rapid stirring and 20- for slow stirring.
It took 40 minutes, but in the present invention, by adopting the loop-shaped flock forming tube, rapid stirring can be 5 to 15 sec., And slow stirring can be about 60 sec., Which can be greatly shortened. Moreover, the floating speed in the floating separation tank is 5 to 8 m in the conventional method.
According to the present invention, the value of / hr becomes 10 to 30 m / hr, and the flotation tank can be made compact. Further, the pressurized residence time of the circulating water is 45 to 90 seconds, compared with 1 to 5 minutes of the conventional method, and the residence time can be greatly shortened.
本発明の浮上分離装置は円筒型のものを図示したが、所
望により角型に設計することも可能である。Although the levitation separation device of the present invention is shown as a cylindrical type, it may be designed in a square type if desired.
次に、本発明を実施例により説明する。 Next, the present invention will be described with reference to examples.
実施例１（加圧浮上分離装置による含油排水の連続処理
実験） 本発明の加圧浮上分離装置を使用してレストランから排
出される含油排水を処理し、油分の除去を行った。実験
条件および実験装置の概要は次の通りである。なお、実
験装置のフローシートは第２図に示したものと同じであ
るが、ループ状フロック形成管は円筒状の浮上分離槽の
外壁に巻きつけた。Example 1 (Continuous treatment experiment of oil-containing wastewater by a pressure floating separator) The oil-containing wastewater discharged from a restaurant was treated using the pressure floating separator of the present invention to remove oil. The experimental conditions and experimental equipment are summarized as follows. The flow sheet of the experimental apparatus is the same as that shown in FIG. 2, but the loop-shaped flock forming tube was wrapped around the outer wall of the cylindrical flotation separation tank.
1.実験条件 処理水 2m3/hr 原水油分濃度 150mg/（平均） 原水SS濃度 135mg/（平均） 原水温度範囲 20/30℃ 目標処理水油分濃度 30mg/以下 2.実験装置概要 浮上分離槽 容 積 200（有効容積180） 寸 法 0.36mφ×1.9mH 滞留時間 5.4分（原水流入量基準） ループ状フロック形成管 急速撹拌部 管 径（内径） 19mmφ 長 さ 12m 緩速撹拌部 管 径（内径） 38mmφ 長 さ 29m 滞留時間 急速撹拌部 5.5sec. 緩速撹拌部 58sec. 凝集剤添加量 ポリ塩化アルミニウム（APC）を原水中に20mg/添加 循環水加圧ポンプ ギアーポンプ 流 量 0.6m3/hr 循環水／原水比 0.6m3/hr/2m3/hr＝0.3 圧 力 5kg/cm2・Ｇ 処理水を循環して用いた。1. Experimental conditions Treated water 2m 3 / hr Raw water oil concentration 150mg / (average) Raw water SS concentration 135mg / (average) Raw water temperature range 20/30 ℃ Target treated water oil concentration 30mg / below 2. Outline of experimental equipment Floating separation tank capacity Product 200 (effective volume 180) Size 0.36mφ × 1.9mH Residence time 5.4 minutes (based on the amount of raw water inflow) Loop-shaped flock forming tube Rapid stirring section Pipe diameter (inner diameter) 19mmφ Length 12m Slow stirring section Pipe diameter (inner diameter) 38mm φ Length 29m Residence time Rapid stirring part 5.5sec. Slow stirring part 58sec. Addition amount of coagulant 20mg / amount of polyaluminum chloride (APC) in raw water Circulating water pressure pump Gear pump Flow rate 0.6m 3 / hr Circulating water / Raw water ratio 0.6m 3 / hr / 2m 3 /hr=0.3 Pressure 5kg / cm 2 · G Treated water was circulated and used.
空気の取り入れ方法および量 加圧ポンプを用いて、吸引側より取り入れる。Intake method and amount of air Take in from the suction side using a pressure pump.
空気取り入れ量 0.06m3/hr 空気／循環水比 0.06/0.6＝0.1 Ｕ字型加圧管 全 長 27m 管 径 21.6mmφ（内径） 上下管の高さ×本数 2.0m×13本 流 速 0.455m/sec. 滞留時間 59sec. 気液分離槽 容 種 2.8 寸 法 80mmφ×560mmH 滞留時間 17sec. 3.結 果 表より明らかなように、本発明の装置を用いて５週間に
わたり連続して含油排水を処理したところ、油分除去率
94％,SS除去率94％という高い値が得られた。Air intake 0.06m 3 / hr Air / circulating water ratio 0.06 / 0.6 ＝ 0.1 U-shaped pressurizing pipe Total length 27m Pipe diameter 21.6mmφ (inner diameter) Height of upper and lower pipes × Number of pipes 2.0m × 13 Flow velocity 0.455m / sec. Residence time 59sec. Gas-liquid separation tank Type 2.8 Dimensions 80mmφ × 560mmH Residence time 17sec. 3.Result As is clear from the table, when the oil-containing wastewater was treated continuously for 5 weeks using the device of the present invention, the oil removal rate was
High values of 94% and SS removal rate of 94% were obtained.
本発明の浮上分離装置によれば、加圧浮上分離法を行う
場合、Ｕ字型加圧管を設けたことにより短時間で加圧水
を製造することができ、またループ状フロック形成管を
設けたことにより短時間でフロックを形成することがで
きる。さらに、原水供給ノズルと循環水供給ノズルの位
置関係を工夫したことにより、原水から浮遊懸濁物や油
分を除去する能力が著しく改善された。従って、本発明
の浮上分離装置を用いれば、原水を短時間に効率よく処
理することができる。According to the levitation separation apparatus of the present invention, when the pressure levitation separation method is performed, it is possible to produce pressurized water in a short time by providing the U-shaped pressure tube, and the loop-shaped flock forming tube is provided. Thus, flocs can be formed in a short time. Furthermore, by devising the positional relationship between the raw water supply nozzle and the circulating water supply nozzle, the ability to remove suspended suspensions and oils from the raw water was significantly improved. Therefore, by using the flotation device of the present invention, raw water can be efficiently treated in a short time.
第１図は、従来の装置を用いる加圧浮上分離法のブロッ
クフローを示す。第２図は、本発明の浮上分離装置を用
いる加圧浮上分離法のフローシートを示す。１原水,2原
水供給ポンプ,3凝集剤タンク,4凝集剤供給ポンプ,5ルー
プ状フロック形成管,6浮上分離槽本体,7回転スカム掻き
取り機,8ドラフトチューブ,9スカム,10原水供給ノズル,
11処理水排出口,12処理水槽,13処理水,14循環水,15空
気,16加圧ポンプ,17コンプレッサー,18U字型加圧管,19
気液分離槽,20空気抜き弁,21加圧循環水,22減圧弁,23循
環水供給ノズルFIG. 1 shows a block flow of a pressure floating separation method using a conventional device. FIG. 2 shows a flow sheet of the pressure levitation separation method using the levitation separation apparatus of the present invention. 1 raw water, 2 raw water supply pump, 3 coagulant tank, 4 coagulant supply pump, 5 loop floc forming tube, 6 flotation separation tank body, 7 rotation scum scraper, 8 draft tube, 9 scum, 10 raw water supply nozzle ,
11 treated water outlet, 12 treated water tank, 13 treated water, 14 circulating water, 15 air, 16 pressurizing pump, 17 compressor, 18 U-shaped pressurizing pipe, 19
Gas-liquid separation tank, 20 air vent valve, 21 pressurized circulating water, 22 pressure reducing valve, 23 circulating water supply nozzle
───────────────────────────────────────────────────── フロントページの続き (72)発明者 高橋 勤 神奈川県横浜市泉区和泉町2219 (72)発明者 若林 中 神奈川県横浜市瀬谷区橋戸３―51―１―16 ―４ (72)発明者 長谷川 潤 神奈川県横浜市港南区港南台９―17 ２― 201 (72)発明者 須永 陽一 神奈川県川崎市宮前区けやき平１番 宮前 平グリーンハイツ１―304 (72)発明者 大西 康史 神奈川県横浜市緑区東本郷６丁目11番 17 ―202号室 (56)参考文献 特開 昭55−104686（ＪＰ，Ａ) 特開 昭61−125479（ＪＰ，Ａ) ─────────────────────────────────────────────────── ─── Continuation of the front page (72) Inventor Tsutomu Takahashi 2219 Izumi-cho, Izumi-ku, Yokohama-shi, Kanagawa (72) Inventor Naka Wakabayashi 3-51-1-1-16-4 (72) Hashido, Seya-ku, Yokohama-shi, Kanagawa Person Jun Hasegawa 9-17, Konandai, Konan-ku, Yokohama-shi, Kanagawa 2-201 (72) Inventor Yoichi Sunaga 1-304 Keyakidaira Miyamae-ku, Miyazaki-ku, Kawasaki-shi, Kanagawa 1-3304 (72) Inventor Yasushi Onishi Yokohama-shi, Kanagawa 6-11-11-202, Higashihongo, Midori-ku Room (56) References JP-A-55-104686 (JP, A) JP-A-61-125479 (JP, A)
Claims (2)
入する液を混ぜる混合部を有し、上部にスカム掻き取り
機とスカム排出口を設け、下部に処理水排出口を設けた
浮上分離槽、内径の小さい第１のチューブと該チューブ
と接続する内径の大きい第２のチューブからなり、気体
の不在下にてフロックを形成せしめるループ状フロック
形成管であって、前記混合部内と連通しており、かつ該
ドラフトチューブ内の先端部に上向きのノズルを取り付
けたフロック形成管、該フロック形成管と接続する原水
供給管、該原水供給管と接続する凝集剤供給手段、前記
処理水排出口と接続しており、処理水抜き出し口と循環
用処理水供給口を有する処理水槽、該循環用処理水供給
口と前記混合部内と連通し、かつ該ドラフトチューブ内
の前記上向きのノズルの直下に下向きに設けた循環水供
給ノズルとを接続する配管、該配管の中間部に設けた互
に連通する複数本のＵ字型加圧管、該Ｕ字型加圧管の上
流側配管と接続する空気供給手段、該Ｕ字型加圧管の下
流側に位置し、該Ｕ字型加圧管および前記配管と接続す
る気液分離槽、該気液分離槽上部に設けた空気抜き弁、
該気液分離槽の下流配管に設けた減圧弁を備えているこ
とを特徴とする浮上分離装置。1. A flotation separation tank having a raw water supply nozzle and a mixing section for mixing liquids flowing in from a circulating water supply nozzle, a scum scraper and a scum discharge port provided at an upper portion, and a treated water discharge port provided at a lower portion. A loop-shaped flock-forming tube which comprises a first tube having a small inner diameter and a second tube having a large inner diameter which is connected to the tube and which forms flocs in the absence of gas, and which communicates with the inside of the mixing section. And a floc forming pipe having an upward nozzle attached to the tip of the draft tube, a raw water supply pipe connected to the flock forming pipe, a coagulant supply means connected to the raw water supply pipe, and the treated water discharge port A treated water tank that is connected and has a treated water outlet and a treated treatment water supply port for circulation, and communicates with the treated treatment water supply port for circulation and the inside of the mixing section, and the upward nozzle in the draft tube. And a plurality of U-shaped pressurizing pipes connected to each other, which are provided in an intermediate portion of the pipe, which are connected to a circulating water supply nozzle provided directly below the pipe, and an upstream pipe of the U-shaped pressurizing pipe. An air supply means to be connected, a gas-liquid separation tank located downstream of the U-shaped pressurizing pipe and connected to the U-shaped pressurizing pipe and the pipe, and an air vent valve provided above the gas-liquid separating tank,
A levitation separation device comprising a pressure reducing valve provided in a downstream pipe of the gas-liquid separation tank.
水供給管およびＵ字型加圧管との接続部と空気供給手段
との接続部の中間に位置する配管にポンプを設置した請
求項１記載の装置。2. A pump is installed in a pipe located in the middle of the connection between the raw water supply pipe and the U-shaped pressurizing pipe on the upstream side of the contact with the coagulant supply means and the connection between the air supply means. The apparatus according to item 1.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1310539A JPH0688018B2 (en) | 1989-12-01 | 1989-12-01 | Flotation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP1310539A JPH0688018B2 (en) | 1989-12-01 | 1989-12-01 | Flotation device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03174292A JPH03174292A (en) | 1991-07-29 |
| JPH0688018B2 true JPH0688018B2 (en) | 1994-11-09 |
Family
ID=18006456
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP1310539A Expired - Fee Related JPH0688018B2 (en) | 1989-12-01 | 1989-12-01 | Flotation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0688018B2 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2573899B2 (en) * | 1992-05-14 | 1997-01-22 | 株式会社エフ・テックス | Purification equipment for rivers, lakes, etc. and oil / water separation equipment |
| JP2796246B2 (en) * | 1994-04-29 | 1998-09-10 | 和泉電気株式会社 | Wastewater treatment equipment |
| NO303048B1 (en) * | 1994-10-19 | 1998-05-25 | Mastrans As | Process and equipment for cleaning a liquid |
| JP6697199B1 (en) * | 2019-07-11 | 2020-05-20 | 株式会社楢崎製作所 | Turbid water treatment device and its treatment method |
| JP7381802B1 (en) * | 2023-07-26 | 2023-11-16 | 義▲隆▼ 小櫻 | Normal pressure flotation treatment method using turbid water treatment equipment |
Family Cites Families (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| PL119699B1 (en) * | 1978-11-20 | 1982-01-30 | Ct Tech Komunal | Installation for water purification,treatment of sewage and contaminated waters and thickening of depositsagrjaznennykh vod,a takzhe sguhhenija osadkov |
| JPS61125479A (en) * | 1984-11-21 | 1986-06-13 | Kurita Water Ind Ltd | Decompression device for pressurized flotation separation equipment |
-
1989
- 1989-12-01 JP JP1310539A patent/JPH0688018B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JPH03174292A (en) | 1991-07-29 |
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