JPH06106170A - Waste water treatment device - Google Patents
Waste water treatment deviceInfo
- Publication number
- JPH06106170A JPH06106170A JP4259263A JP25926392A JPH06106170A JP H06106170 A JPH06106170 A JP H06106170A JP 4259263 A JP4259263 A JP 4259263A JP 25926392 A JP25926392 A JP 25926392A JP H06106170 A JPH06106170 A JP H06106170A
- Authority
- JP
- Japan
- Prior art keywords
- water
- treated
- ion exchange
- treatment
- 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.)
- Withdrawn
Links
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- Water Treatment By Sorption (AREA)
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Treatment Of Water By Ion Exchange (AREA)
- Removal Of Specific Substances (AREA)
Abstract
Description
【０００１】[0001]
【産業上の利用分野】本発明は、フッ素系界面活性剤を
含んでなる表面洗浄排水を処理する装置に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to an apparatus for treating surface cleaning waste water containing a fluorine-containing surfactant.
【０００２】[0002]
【従来の技術】従来、半導体や磁気ディスクなどの精密
洗浄および各種機械や部品の脱脂洗浄などの表面洗浄剤
として広くフロン溶剤が使用されてきたが、フロンが地
球のオゾン層を破壊するおそれがあるとしてその使用が
禁止される方向にあり、最近ではフロン溶剤に代わって
特殊なフッ素系界面活性剤が用いられている。一般的な
炭化水素系の界面活性剤では洗浄効果がフロン溶剤に及
ばないが、このフッ素系界面活性剤は、フロン溶剤以上
の洗浄効果を奏するので使用量が増加する傾向にある。2. Description of the Related Art Conventionally, a CFC solvent has been widely used as a surface cleaning agent for precision cleaning of semiconductors and magnetic disks and degreasing cleaning of various machines and parts. However, CFCs may destroy the ozone layer of the earth. However, its use is prohibited, and recently, a special fluorine-based surfactant has been used instead of a CFC solvent. A general hydrocarbon-based surfactant does not have a cleaning effect on a CFC solvent, but this fluorine-based surfactant has a cleaning effect equal to or higher than that of a CFC solvent, and therefore the amount used tends to increase.
【０００３】このフッ素系界面活性剤はパーフルオロア
ルキル基を有する界面活性剤であり、たとえばパーフル
オロアルキルリン酸エステル（アニオン性界面活性
剤）、およびパーフルオロアルキルカルボン酸塩（アニ
オン性界面活性剤）などがあげられる。また、パーフル
オロアルキル基を含むカチオン性界面活性剤も用いられ
る。これらは解離性界面活性剤である。This fluorine-containing surfactant is a surfactant having a perfluoroalkyl group, such as perfluoroalkyl phosphate ester (anionic surfactant) and perfluoroalkylcarboxylic acid salt (anionic surfactant). ) And so on. Further, a cationic surfactant containing a perfluoroalkyl group is also used. These are dissociative surfactants.
【０００４】これらのフッ素系界面活性剤は、表面洗浄
装置において、通常、0.1 ％程度の濃度で表面洗浄水に
含まれ被処理体の表面の洗浄に用いられる。被処理体
は、被処理体に表面洗浄水を循環して噴射することによ
り表面洗浄される。ここで使用された表面洗浄水、ある
いはさらに純水によるすすぎ洗の洗浄水が加わって、排
水処理すべき液体が形成される。In the surface cleaning apparatus, these fluorine-containing surfactants are usually contained in surface cleaning water at a concentration of about 0.1% and used for cleaning the surface of the object to be treated. The surface of the object to be processed is cleaned by circulating and spraying surface cleaning water on the object to be processed. The surface cleaning water used here or the cleaning water for rinsing with pure water is further added to form a liquid to be treated for waste water.
【０００５】表面洗浄装置から排出される排水の水質
は、使用されたフッ素系界面活性剤による以外に被処理
体の汚れの程度により大幅に変動するが、一般的に半導
体やディスクのような精密洗浄のばあいは、使用された
フッ素系界面活性剤以外の排水中に含まれる水質汚染物
質の量は少ない。これに対し、脱脂洗浄のばあいは、フ
ッ素系界面活性剤以外の油などの表面付着物が排水中に
多量に含まれ水質汚濁が生ずる。The quality of the waste water discharged from the surface cleaning device varies greatly depending on the degree of contamination of the object to be treated, in addition to the fluorine-based surfactant used, but in general, precision such as that of semiconductors and disks is high. In the case of washing, the amount of water pollutants contained in the wastewater other than the used fluorosurfactant is small. On the other hand, in the case of degreasing cleaning, a large amount of surface deposits such as oil other than the fluorine-based surfactant is contained in the waste water, resulting in water pollution.
【０００６】これらの排水は、環境汚染につながるの
で、いかなる規模の工場からの排水も排水処理装置によ
り排水処理されなくてはならない。Since these wastewaters lead to environmental pollution, wastewaters from factories of any size must be treated with wastewater treatment equipment.
【０００７】大規模工場では、表面洗浄装置からの原水
の排出量は多いが、たとえば凝集処理槽、生物処理槽お
よび活性炭吸着塔を備える排水処理設備を有しており、
原水をそのまま、または他の排水に混合して、このよう
な大規模の排水処理設備で処理することができる。A large-scale factory has a large amount of raw water discharged from the surface cleaning device, but has a wastewater treatment facility including, for example, a coagulation treatment tank, a biological treatment tank and an activated carbon adsorption tower,
Raw water can be treated as it is or mixed with other wastewater in such a large-scale wastewater treatment facility.
【０００８】[0008]
【発明が解決しようとする課題】これに対し、表面洗浄
装置の排水量が１ｍ3 ／日未満の小型の表面洗浄装置を
用いる小さな工場では、生物処理槽を備える排水処理設
備を設けることは困難である。なぜなら、生物処理槽
は、１日の排水量とほぼ同容積以上の曝気槽が必要であ
るので広い設置場所を必要とし、この排水処理のために
生物処理槽を利用することは非経済的であるからであ
る。また、排水が定常的に流れず数日間滞留すると処理
微生物の活性が低下し処理能力を喪失するので、生物処
理槽は排水量の少ない小さな工場には適さない。On the other hand, in a small factory that uses a small surface cleaning device whose surface cleaning device discharges less than 1 m 3 / day, it is difficult to install a wastewater treatment facility equipped with a biological treatment tank. is there. This is because the biological treatment tank requires an aeration tank with a volume equal to or more than the volume of wastewater per day, so a wide installation area is required, and it is uneconomical to use the biological treatment tank for this wastewater treatment. Because. Moreover, the biological treatment tank is not suitable for a small factory with a small amount of wastewater because the activity of the treated microorganisms decreases and the treatment capacity is lost if the wastewater does not flow constantly and stays for several days.
【０００９】本発明は前記問題点に鑑みなされたもので
あり、その目的は、排水処理すべき原水の排水量の少な
い小さな工場でも問題なく利用できる、小型の処理装置
を提供することにある。The present invention has been made in view of the above problems, and an object thereof is to provide a small-sized treatment apparatus which can be used without problems even in a small factory with a small amount of discharged raw water to be treated.
【００１０】[0010]
【課題を解決するための手段】本発明の前記目的は、フ
ッ素系界面活性剤を含んでなる洗浄排水を処理する装置
であって、該排水に凝集剤を加えて凝集処理する凝集処
理槽と、凝集処理槽内で形成された凝集物を濾過除去す
るためのカートリッジ式濾過器と、濾過器よりの濾液か
らイオン性物質を除去するための陰イオン交換樹脂と陽
イオン交換樹脂を混合して含む混床式イオン交換塔とが
１つの枠内に組み込まれてなる排水処理装置による解決
される。The above object of the present invention is an apparatus for treating cleaning wastewater containing a fluorosurfactant, and a coagulation treatment tank for coagulating the wastewater with a coagulant. A mixture of a cartridge type filter for removing aggregates formed in the aggregating tank and an anion exchange resin and a cation exchange resin for removing ionic substances from the filtrate from the filter. And a mixed bed type ion exchange tower including the same are incorporated into one frame to solve the problem.
【００１１】[0011]
【作用】本発明の排水処理装置は、イオン性物質の除去
のために嵩高い生物処理槽の代わりに小さな混床式イオ
ン交換塔を用いるので、設置面積が少なくてすみ、ま
た、断続的使用も可能になる。また、生物処理は時間が
かかるが混床式イオン交換塔による処理時間は短いので
排水処理時間が短縮される。また、形成された凝集物の
濾過のためにカートリッジ式濾過器を用いることによっ
ても嵩が小さくなっている。さらに、装置全体が所定の
枠内に収められているので搬送も容易である。The wastewater treatment equipment of the present invention uses a small mixed bed type ion exchange column instead of a bulky biological treatment tank for the removal of ionic substances, so the installation area is small and intermittent use is possible. Will also be possible. In addition, although biological treatment takes time, the treatment time by the mixed bed type ion exchange tower is short, so the wastewater treatment time is shortened. Also, the bulk is reduced by using a cartridge type filter for filtering the formed aggregate. Further, since the entire device is housed in a predetermined frame, it can be easily transported.
【００１２】[0012]
【実施例】本発明の排水処理装置において原水はつぎの
ように処理される。まず、凝集処理槽に排水処理すべき
原水を流入させる。そこに所定量の凝集剤が投入され、
凝集物が形成される。この凝集処理槽では、フッ素系界
面活性剤以外の水質汚濁物質や、油などの被処理体の表
面除去物、固体物が凝集される。この凝集物を含む被処
理液がカートリッジ式濾過器に送られ、凝集物がカート
リッジ式濾過器により濾去される。凝集物が除かれた被
処理液は混床式イオン交換塔に送られて解離性のフッ素
系界面活性剤、その他のイオンが除去される。フッ素系
界面活性剤が除去されたのちの処理液は純水に近く、放
流しても問題なく、水として再利用することをも可能で
ある。EXAMPLE Raw water is treated in the wastewater treatment equipment of the present invention as follows. First, raw water to be treated as waste water is made to flow into the coagulation tank. A predetermined amount of coagulant is added there,
Aggregates are formed. In this coagulation treatment tank, water pollutants other than the fluorine-based surfactant, surface-removed substances such as oil, and solid substances are aggregated. The liquid to be treated containing the aggregate is sent to the cartridge type filter, and the aggregate is filtered off by the cartridge type filter. The liquid to be treated from which the agglomerates have been removed is sent to a mixed bed type ion exchange column to remove the dissociative fluorine-based surfactant and other ions. The treatment liquid after the removal of the fluorosurfactant is close to pure water, and it can be reused as water without any problem even if it is discharged.
【００１３】本発明の排水処理装置の一実施態様を図１
に示す。また、図１の装置の構成を示す図を図２に示
す。FIG. 1 shows an embodiment of the waste water treatment apparatus of the present invention.
Shown in. 2 is a diagram showing the configuration of the apparatus shown in FIG.
【００１４】図１において、１は凝集処理槽、２はカー
トリッジ式濾過器、３は混床式イオン交換塔、４は攪拌
ブロワー、５は制御盤、６は排水処理装置の枠、７、８
および９はそれぞれ薬品計量器を示す。図２において、
１〜９は図１と同様のものを示し、10は処理ポンプ、11
は処理すべき排水すなわち原水を一時的に貯蔵する更新
液槽、12は原水受入ポンプ（ハンデーポンプ）、13は放
流側溝を示す。In FIG. 1, 1 is a flocculation treatment tank, 2 is a cartridge type filter, 3 is a mixed bed type ion exchange tower, 4 is a stirring blower, 5 is a control panel, 6 is a frame of a waste water treatment device, and 7 and 8.
Reference numerals 9 and 9 respectively indicate a chemical measuring instrument. In FIG.
1-9 shows the same thing as FIG. 1, 10 is a processing pump, 11
Is a renewal liquid tank for temporarily storing wastewater to be treated, that is, raw water, 12 is a raw water receiving pump (handy pump), and 13 is a discharge side groove.
【００１５】図１の排水処理装置における排水処理の主
要部分の好ましい態様についてつぎに説明する。A preferred embodiment of the main part of wastewater treatment in the wastewater treatment equipment of FIG. 1 will be described below.
【００１６】（１）凝集処理槽１における処理 凝集処理槽１に更新液槽11から原水を原水受入ポンプ12
を用いて入れる。空気曝気しながら、薬品計量器７から
硫酸アルミニウムを含む液体硫酸バント液（酸化アルミ
ニウムとして８％濃度）（または塩化第二鉄液（39％濃
度）もしくはポリ塩化アルミニウム液（酸化アルミニウ
ムとして10％濃度））を注入し、つぎに薬品計量器８か
らの約５％水酸化ナトリウム水溶液で（または他のアル
カリ剤を用いて）ｐＨを6.5 〜8.0 にし、つぎに薬品計
量器９から高分子凝集剤（リューフロックA-101(大日本
インキ化学工業（株）製))を添加して凝集を生じさせ
る。(1) Treatment in the coagulation treatment tank 1 The coagulation treatment tank 1 receives raw water from the renewal liquid tank 11 and the raw water receiving pump 12
Use to insert. Liquid aeration solution containing aluminum sulfate (8% concentration as aluminum oxide) (or ferric chloride solution (39% concentration) or polyaluminum chloride solution (10% concentration as aluminum oxide) while aeration with air. )) Is injected, and then the pH is adjusted to 6.5 to 8.0 with an approximately 5% aqueous sodium hydroxide solution from the chemical measuring instrument 8 (or using another alkaline agent), and then the polymer coagulant from the chemical measuring instrument 9 is added. (Ruflock A-101 (manufactured by Dainippon Ink and Chemicals, Inc.)) is added to cause aggregation.
【００１７】（２）カートリッジ式濾過器２における処
理 交換部品であるカートリッジ式濾過筒のフィルターとし
て、繊毛をもたせたヤーンをプラスチック製中心筒（コ
アー）に巻き付けた一般的なフィルターを使用する。濾
過器２の濾過入口と濾過出口に水圧計を取り付ける。処
理ポンプ10により供給された凝集物を含む被処理液をフ
ィルターで連続濾過する。濾過孔が目詰まりして濾過差
圧が大きくなるにしたがって、濾過能力が低下し、遂に
は濾過困難な状態になるので、その前にカートリッジ式
濾過筒を新品と交換する。(2) Treatment in Cartridge Type Filter 2 As a filter of a cartridge type filtering cylinder which is a replacement part, a general filter in which a yarn having cilia is wound around a plastic central cylinder (core) is used. A water pressure gauge is attached to the filtration inlet and the filtration outlet of the filter 2. The liquid to be treated containing the aggregates supplied by the treatment pump 10 is continuously filtered with a filter. As the filtration hole becomes clogged and the filtration pressure difference increases, the filtration capacity decreases, and finally the filtration becomes difficult. Therefore, before that, replace the cartridge filtration tube with a new one.
【００１８】凝集処理槽で発生した凝集物は全てカート
リッジ式濾過筒に捕捉され、カートリッジ式濾過筒は産
業廃棄物として処理される。よって、生物処理槽を利用
したばあいに生じる活性汚泥処理のような余剰汚泥の処
理は必要ない。All the agglomerates generated in the aggregating treatment tank are captured by the cartridge type filter cylinder, and the cartridge type filter cylinder is treated as industrial waste. Therefore, it is not necessary to treat surplus sludge such as activated sludge treatment that occurs when a biological treatment tank is used.
【００１９】（３）混床式イオン交換塔３における処理 イオン交換樹脂はあらかじめＨ型に賦活した強カチオン
交換樹脂（デュオライトＣ−20（デュポン社製））とＯ
Ｈ型に賦活した強アニオン交換樹脂（デュオライトＡ−
101 Ｄ（デュポン社製））を容量基準で１：９〜９：１
の範囲内の混合比で均一に混合したものをイオン交換塔
に充填し、通常のイオン交換純水製造装置と同じように
使用する。イオン交換水の出口側に電気伝導率計を取り
付け、常時水質を監視する。通水は下向流、上向流のい
ずれでもよいが、下向流が一般的である。樹脂に対する
イオン交換通水速度を空塔速度５〜15リットル／樹脂リ
ットル／Ｈｒとして、カートリッジ式濾過器に通水す
る。通水時間の経過とともに、通水液中の無機イオンお
よび解離性の界面活性剤などのイオン交換が進行する
と、これらの吸着イオン帯が通水入口側から出口側に向
かって徐々に拡大し、遂にはイオン交換能力が低下し、
出口側からイオンがリークし始める。イオンがリークし
始めるとイオン交換処理水の電気伝導率が徐々に上昇す
るので、目的とする水質限界の電気伝導率を決めて、感
知し、目的の値になった時点でイオン交換樹脂を取り出
し、新しいイオン交換樹脂を充填する。使用済のイオン
交換樹脂は産業廃棄物として処分するか、または再生し
て繰り返し使用してよい。(3) Treatment in the mixed bed type ion exchange tower 3 The ion exchange resin is a strong cation exchange resin (Duolite C-20 (manufactured by DuPont)) which has been activated to H type in advance, and O.
Strong anion exchange resin activated to H type (Duolite A-
101D (manufactured by DuPont) 1: 9 to 9: 1 based on capacity
A mixture uniformly mixed with a mixing ratio within the range is packed in an ion exchange column and used in the same manner as an ordinary ion exchange pure water production apparatus. An electric conductivity meter is installed on the outlet side of ion-exchanged water to constantly monitor the water quality. The water flow may be either downward flow or upward flow, but downward flow is common. The ion exchange water flow rate to the resin is 5 to 15 liters of superficial column velocity / resin liter / Hr, and water is passed through the cartridge type filter. With the passage of water passage time, when ion exchange of inorganic ions in the water passage liquid and dissociative surfactant progresses, these adsorbed ion bands gradually expand from the water inlet side toward the outlet side, Eventually the ion exchange capacity declines,
Ions start to leak from the exit side. When the ions start to leak, the electric conductivity of the ion-exchanged water gradually rises, so determine the electric conductivity of the target water quality limit, sense it, and take out the ion-exchange resin when the target value is reached. , Fill with new ion exchange resin. The used ion-exchange resin may be disposed of as industrial waste, or may be recycled and reused.
【００２０】このイオン交換処理水は、解離性のイオン
が完全に除去されて純水に近いので、ｐＨが排水規制の
5.8 〜8.6 の範囲内に収まり、そのまま放流側溝13に放
流可能である。Since the dissociative ions are completely removed and the ion-exchanged water is close to pure water, the pH of the water is regulated by waste water.
It falls within the range of 5.8 to 8.6 and can be discharged to the discharge gutter 13 as it is.
【００２１】この混床式イオン交換塔３によれば陰イオ
ンおよび陽イオン性物質の両方が除去される。According to the mixed bed type ion exchange column 3, both anions and cationic substances are removed.
【００２２】本発明において、被処理液中の不純物をさ
らに取り除くために、カートリッジ式濾過器と混床式イ
オン交換塔との間にさらに活性炭吸着塔を設けてよい。
そのばあいの本発明の排水処理装置の構成を図３に示
す。図３中、符号１〜13は図２と同じものを示し、14は
さらに設けられた活性炭吸着塔を示す。In the present invention, in order to further remove impurities in the liquid to be treated, an activated carbon adsorption column may be further provided between the cartridge type filter and the mixed bed type ion exchange column.
In that case, the structure of the waste water treatment apparatus of the present invention is shown in FIG. In FIG. 3, reference numerals 1 to 13 are the same as those in FIG. 2, and 14 is a further activated carbon adsorption tower.
【００２３】本発明によれば、300 リットルの凝集処理
槽と20リットルの混床式イオン交換塔とを組み合わせた
とき、１ｍ3 ／日の処理能力をもち、コンパクトで高性
能の装置を提供できる。凝集処理槽は要求される処理能
力や設置空間によって異なるが100 〜500 リットルの容
量のものに設計でき、カートリッジ式濾過器はフィルタ
ーの長さ250mm 、径61mmのものを１〜24本組合せたもの
に設計でき、混床式イオン交換塔は５〜40リットルの容
量のものに設計でき、活性炭吸着塔は５〜40リットルの
容量のものに設計できる。According to the present invention, when a coagulation treatment tank of 300 liters and a mixed bed type ion exchange tower of 20 liters are combined, a processing capacity of 1 m 3 / day, a compact and high performance apparatus can be provided. . The coagulation tank can be designed to have a capacity of 100 to 500 liters depending on the required processing capacity and installation space, and the cartridge type filter is a combination of 1 to 24 filters with a filter length of 250 mm and a diameter of 61 mm. The mixed bed ion exchange tower can be designed to have a capacity of 5 to 40 liters, and the activated carbon adsorption tower can be designed to have a capacity of 5 to 40 liters.
【００２４】つぎに、本発明の排水処理装置を用いて具
体的に排水処理を行なった例を示す。Next, an example of concrete wastewater treatment using the wastewater treatment apparatus of the present invention will be shown.
【００２５】実施例１ 図１に示すような本発明の排水処理装置およびつぎの生
物的排水処理装置を用いて原水の排水処理を行なった。Example 1 Wastewater treatment of raw water was carried out using the wastewater treatment equipment of the present invention and the following biological wastewater treatment equipment as shown in FIG.
【００２６】この生物的排水処理装置は、１日４回バッ
チ処理することにより１日に400 リットル排水処理する
ものであり、凝集処理槽の容量が100 リットル、生物処
理槽の容量が500 リットル、生物処理槽からの活性汚泥
を除くための沈殿分離槽の容量が50リットルであり、装
置全体の大きさがタテ2000mm×ヨコ2000mm×高さ2000mm
である。また図１の本発明の排水処理装置も、１日４回
バッチ処理することにより１日に400 リットルの排水処
理を行なうものであるが、凝集処理槽の容量が150 リッ
トル、カートリッジ式濾過器のフィルターの長さ250mm
、径61mmのものが６本が一つの濾過器内に組合された
もの、混床式イオン交換塔の樹脂全量が10リットルであ
り、装置全体の大きさがタテ900mm ×ヨコ1000mm×高さ
1500mmとコンパクトである。This biological wastewater treatment equipment is capable of treating 400 liters of wastewater by batch processing four times a day. The coagulation treatment tank has a capacity of 100 liters, and the biological treatment tank has a capacity of 500 liters. The sedimentation tank for removing activated sludge from the biological treatment tank has a capacity of 50 liters, and the overall size of the device is vertical 2000 mm × horizontal 2000 mm × height 2000 mm.
Is. The waste water treatment apparatus of the present invention shown in FIG. 1 also performs waste water treatment of 400 liters a day by batch processing four times a day, but the coagulation treatment tank has a capacity of 150 liters and a cartridge type filter. Filter length 250mm
, 6 pieces of diameter 61mm are combined in one filter, the total amount of resin of the mixed bed type ion exchange tower is 10 liters, and the size of the whole device is vertical 900mm × horizontal 1000mm × height
Compact with 1500 mm.
【００２７】原水としては、表面洗浄剤（（パーフルオ
ロアルキルリン酸エステル）0.1 ％水溶液）を用いて磁
気装置などを精密洗浄した排水を用いた。この原水の特
性を表１に示す。As the raw water, waste water obtained by precision cleaning of a magnetic device and the like using a surface cleaning agent ((perfluoroalkyl phosphate ester) 0.1% aqueous solution) was used. The characteristics of this raw water are shown in Table 1.
【００２８】[0028]
【表１】 [Table 1]
【００２９】この本発明の排水処理装置を用いてつぎの
ように原水を排水処理した。まず、凝集処理槽１に更新
液槽11から原水100 リットルを原水受入ポンプ12を用い
て入れた。空気曝気しながら、容量15リットルの薬品計
量器７から液体硫酸バント液（住友化学工業（株）製）
70ｍｌを注入し、つぎに薬品計量器８から約５％水酸化
ナトリウム水溶液を加えてｐＨを７にし、続いて薬品計
量器９から高分子凝集剤（リューフロックＡ−101 （大
日本インキ化学工業（株）製）0.1 ％水溶液）400 ｍｌ
を添加して凝集を生じさせた。凝集物を含む被処理液を
処理ポンプ10によりカートリッジ式濾過器２（ＣＦＨ−
６ＡＢＨ（セントラルフィルター（株）製））に送り、
凝集物を濾去した。凝集物が濾去された被処理液を、強
カチオン交換樹脂（デュオライトＣ−20）と強アニオン
交換樹脂（デュオライトＡ−101Ｄ）とを１：１の容量
比で含む混床式イオン交換塔３（カートリッジ式純水製
造装置（オルガノ（株）製））に空塔速度10で通水して
イオン性物質を除去した。Using the wastewater treatment equipment of the present invention, raw water was treated as follows. First, 100 liters of raw water was put into the coagulation treatment tank 1 from the renewal liquid tank 11 using the raw water receiving pump 12. Liquid aeration bunto liquid (manufactured by Sumitomo Chemical Co., Ltd.) from a chemical meter 7 with a capacity of 15 liters while aerating air.
Inject 70 ml, and then add about 5% sodium hydroxide aqueous solution from the chemical measuring instrument 8 to adjust the pH to 7. Then, from the chemical measuring instrument 9, the polymer flocculant (Leuflock A-101 (Dainippon Ink and Chemicals) Co., Ltd.) 0.1% aqueous solution) 400 ml
Was added to cause agglomeration. The liquid to be treated containing agglomerates is filtered by the treatment pump 10 into a cartridge type filter 2 (CFH-
Send to 6ABH (Central Filter Co., Ltd.),
The aggregate was filtered off. Mixed bed type ion exchange containing a strong cation exchange resin (Duolite C-20) and a strong anion exchange resin (Duolite A-101D) in a volume ratio of 1: 1 in the liquid to be treated from which the agglomerates have been filtered off. Ionic substances were removed by passing water through a tower 3 (cartridge type pure water producing apparatus (manufactured by Organo Co.)) at a superficial velocity of 10.
【００３０】また、前記従来の排水処理装置を用いた原
水の排水処理は一般的な従来の手順にしたがって行なっ
た。Further, the wastewater treatment of raw water using the conventional wastewater treatment equipment was carried out according to a general conventional procedure.
【００３１】本発明の前記排水処理装置を用いた処理方
法および従来の前記排水処理装置を用いた処理方法によ
る精密清浄排水としての原水の排水処理の結果を表２に
示す。表２には、凝集処理により生じた凝集物を濾去し
た後の濾過水と、最終的な被処理液（従来の処理方法に
おいては生物処理槽で生じた活性汚泥たる沈殿物を分離
した後の上澄液、本発明の処理方法においては混床式イ
オン交換塔から排出されるイオン交換処理水）について
測定した各種データを示す。なお最終的な被処理液を得
るまでの処理時間は、本発明の装置では７時間、従来の
装置では24時間であった。Table 2 shows the results of wastewater treatment of raw water as precision clean wastewater by the treatment method using the wastewater treatment equipment of the present invention and the conventional treatment method using the wastewater treatment equipment. Table 2 shows the filtered water after filtering off the agglomerates generated by the agglomeration treatment and the final liquid to be treated (in the conventional treatment method, after separating the precipitates which are the activated sludge generated in the biological treatment tanks). The above shows various data measured for the supernatant, the ion-exchange treated water discharged from the mixed bed type ion-exchange tower in the treatment method of the present invention. The processing time until the final liquid to be treated was 7 hours in the apparatus of the present invention and 24 hours in the conventional apparatus.
【００３２】[0032]
【表２】 [Table 2]
【００３３】表２に示すように、本発明の処理方法によ
れば、凝集物の濾去後のそのつぎの被処理液の処理のた
めに生物処理槽ではなく混床式イオン交換塔を用いたこ
とにより、被処理液のＣＯＤおよびＢＯＤが大きく低下
する。ヘキサン抽出物質量は、凝集物を濾去した時点に
おいてすでに従来技術と同等に少なくなる。また、被処
理液のｐＨも問題のない範囲に収まる。さらに、本発明
の処理方法によれば、電気伝導率が大きく低下すること
から、混床式イオン交換塔によりイオン性物質のほとん
どが除去されることがわかる。As shown in Table 2, according to the treatment method of the present invention, a mixed bed type ion exchange column is used instead of the biological treatment tank for the treatment of the next liquid to be treated after filtering off the agglomerates. As a result, the COD and BOD of the liquid to be treated are greatly reduced. The amount of hexane extract material is already as low as in the prior art when the aggregates are filtered off. In addition, the pH of the liquid to be treated falls within a range without any problem. Further, according to the treatment method of the present invention, since the electric conductivity is greatly reduced, it can be seen that most of the ionic substances are removed by the mixed bed type ion exchange column.
【００３４】実施例２ 図３に示すような本発明の排水処理装置および前記生物
的排水処理装置を用いて原水の排水処理を行なった。Example 2 Wastewater treatment of raw water was carried out using the wastewater treatment equipment of the present invention and the biological wastewater treatment equipment as shown in FIG.
【００３５】この本発明の排水処理装置は、活性炭吸着
塔の活性炭量が10リットルである以外は実施例１で用い
た本発明の装置と同じ寸法のものであり、１日の処理量
も実施例１で用いた本発明の装置と同じであるが、装置
全体の大きさはタテ1000mm×ヨコ1300mm×高さ1500mmで
ある。ここで用いた従来の排水処理装置は実施例１で用
いた従来装置の生物処理槽にさらに活性炭量10リットル
の活性炭吸着塔が接続されたものであり全体の大きさは
タテ2000mm×ヨコ2000mm×高さ2000mmである。This wastewater treatment equipment of the present invention has the same size as the equipment of the present invention used in Example 1 except that the amount of activated carbon in the activated carbon adsorption tower is 10 liters, and the amount of treatment per day is also carried out. It is the same as the device of the present invention used in Example 1, but the overall size of the device is 1000 mm in length × 1300 mm in width × 1500 mm in height. The conventional wastewater treatment equipment used here is the biological treatment tank of the conventional equipment used in Example 1 to which an activated carbon adsorption tower with an activated carbon amount of 10 liters is further connected, and the overall size is vertical 2000 mm × horizontal 2000 mm × The height is 2000 mm.
【００３６】原水としては、表面処理剤（パーフルオロ
アルキルリン酸エステル 0.1％水溶液）を用いて一般機
械などを脱脂洗浄した排水を用いた。この原水の特性を
表１に示す。As raw water, waste water obtained by degreasing and washing general machinery using a surface treatment agent (0.1% aqueous solution of perfluoroalkyl phosphate) was used. The characteristics of this raw water are shown in Table 1.
【００３７】この本発明の排水処理装置を用いて、活性
炭吸着塔14で不純物をさらに除去した以外は実施例１の
本発明の排水処理装置による排水処理と同じ手順により
原水を処理した。また、従来の排水処理装置について
は、一般的な従来の手順にしたがって最後に活性炭吸着
塔で不純物を除去して排水処理を行なった。Using this wastewater treatment apparatus of the present invention, raw water was treated by the same procedure as the wastewater treatment by the wastewater treatment apparatus of the present invention of Example 1 except that impurities were further removed in the activated carbon adsorption tower 14. Regarding the conventional wastewater treatment equipment, finally, according to the general conventional procedure, impurities were removed in the activated carbon adsorption tower to perform wastewater treatment.
【００３８】これらの排水処理の結果を表３に示す。本
発明の処理方法については、凝集処理により生じた凝集
物を濾去した後の濾過水（カートリッジ式濾過器２から
の被処理液）と、活性炭吸着塔通水処理水（さらに設け
られた活性炭吸着塔14からの被処理液）と、イオン交換
水（混床式イオン交換塔３からの被処理液）とについて
測定した各種データを表３に示す。従来の処理方法につ
いては、凝集処理により生じた凝集物を濾去した後の濾
過水と、生物処理槽で生じた活性汚泥たる沈殿物を分離
した後の上澄液と、さらにこの上澄液を別の活性炭吸着
塔を通水させた処理水とについて測定した各種データを
表３に示す。なお、最終的な被処理液が得られるまでの
排水処理時間は、本発明の装置では７時間、従来の装置
では24時間であった。Table 3 shows the results of these wastewater treatments. Regarding the treatment method of the present invention, the filtered water (the liquid to be treated from the cartridge type filter 2) after filtering off the agglomerates generated by the agglomeration treatment, and the activated carbon adsorption tower water treatment treated water (further provided activated carbon Table 3 shows various data measured for the liquid to be treated from the adsorption tower 14 and the ion-exchanged water (the liquid to be treated from the mixed bed type ion-exchange tower 3). Regarding the conventional treatment method, the filtered water after filtering off the agglomerates generated by the agglomeration treatment, the supernatant after separating the precipitate which is the activated sludge generated in the biological treatment tank, and further this supernatant Table 3 shows various data measured for the treated water obtained by passing water through another activated carbon adsorption tower. The wastewater treatment time until the final liquid to be treated was 7 hours in the apparatus of the present invention and 24 hours in the conventional apparatus.
【００３９】[0039]
【表３】 [Table 3]
【００４０】図３に示すように、さらに活性炭吸着塔14
を設けることにより、油やその他表面付着物に起因する
水質汚濁物質が多い機械加工などの脱脂洗浄排水でも、
精密洗浄排水と同程度の処理水質まで処理することがで
きる。また、この活性炭吸着処理後イオン交換処理され
ることになるので、イオン交換樹脂の表面汚染が軽減で
き、樹脂を再生して繰返し長期間使用することができ経
済的である。As shown in FIG. 3, an activated carbon adsorption tower 14 is further provided.
By installing, even degreasing cleaning drainage such as machining where there are many water pollutants due to oil and other surface deposits,
It can treat up to the same level of treated water as precision-cleaned wastewater. Further, since the ion exchange treatment is carried out after the activated carbon adsorption treatment, the surface contamination of the ion exchange resin can be reduced and the resin can be regenerated and repeatedly used for a long time, which is economical.
【００４１】[0041]
【発明の効果】本発明の排水処理装置は、大きな生物処
理槽を用いず、濾過器としてカートリッジ式濾過器を用
いるので、全体としての寸法が小さく設置面積が少なく
てすむ。また、生物処理槽を用いたばあいに生じる運転
停止時の処理微生物の活性低下による処理能力の喪失の
問題が生じない。したがって原水排水量が少ない小規模
の工場において用いるのに適している。また生物処理を
用いないため、排水処理時間が生物処理槽を備える従来
の排水処理装置より短くてすむ。Since the wastewater treatment equipment of the present invention does not use a large biological treatment tank but uses a cartridge type filter as a filter, the overall size is small and the installation area is small. In addition, there is no problem of loss of processing ability due to a decrease in the activity of the processing microorganisms when the operation is stopped, which occurs when a biological processing tank is used. Therefore, it is suitable for use in small-scale factories with low raw water discharge. Further, since the biological treatment is not used, the wastewater treatment time can be shorter than that of the conventional wastewater treatment equipment having the biological treatment tank.
【図１】本発明の排水処理装置の断面図である。FIG. 1 is a cross-sectional view of a wastewater treatment device of the present invention.
【図２】図１の排水処理装置の構成を示す模式図であ
る。FIG. 2 is a schematic diagram showing the configuration of the wastewater treatment device of FIG.
【図３】本発明のもう一つの排水処理装置の構成を示す
模式図である。FIG. 3 is a schematic diagram showing the configuration of another waste water treatment apparatus of the present invention.
１ 凝集措置槽 ２ カートリッジ式濾過器 ３ 混床式イオン交換塔 ４ 攪拌ブロワー ５ 制御盤 ６ 枠 ７ 薬品計量器 ８ 薬品計量器 ９ 薬品計量器 10 処理ポンプ 11 更新液槽 12 原水受入ポンプ 13 放流側溝 14 活性炭吸着塔 1 Coagulation Measure Tank 2 Cartridge Filter 3 Mixed Bed Type Ion Exchange Tower 4 Stirring Blower 5 Control Panel 6 Frame 7 Chemicals Meter 8 Chemicals Meter 9 Chemicals Meter 10 Processing Pump 11 Renewal Liquid Tank 12 Raw Water Intake Pump 13 Discharge Side Gutter 14 Activated carbon adsorption tower
Claims (2)
水を処理する装置であって、該排水に凝集剤を加えて凝
集処理する凝集処理槽と、凝集処理槽内で形成された凝
集物を濾過除去するためのカートリッジ式濾過器と、濾
過器よりの濾液からイオン性物質を除去するための陰イ
オン交換樹脂と陽イオン交換樹脂を混合して含む混床式
イオン交換塔とが１つの枠内に組み込まれてなる排水処
理装置。1. An apparatus for treating cleaning wastewater containing a fluorosurfactant, which comprises an aggregating tank for aggregating by adding an aggregating agent to the wastewater, and an aggregate formed in the aggregating tank. And a mixed bed type ion exchange column for mixing cation exchange resin and anion exchange resin for removing ionic substances from the filtrate from the filter. Wastewater treatment equipment built into the frame.
換塔の間にさらに活性炭吸着塔が接続された請求項１記
載の排水処理装置。2. The wastewater treatment apparatus according to claim 1, further comprising an activated carbon adsorption tower connected between the cartridge type filter and the mixed bed type ion exchange tower.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4259263A JPH06106170A (en) | 1992-09-29 | 1992-09-29 | Waste water treatment device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP4259263A JPH06106170A (en) | 1992-09-29 | 1992-09-29 | Waste water treatment device |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH06106170A true JPH06106170A (en) | 1994-04-19 |
Family
ID=17331680
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP4259263A Withdrawn JPH06106170A (en) | 1992-09-29 | 1992-09-29 | Waste water treatment device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH06106170A (en) |
Cited By (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005161224A (en) * | 2003-12-03 | 2005-06-23 | Fujita Corp | Calcium removing method and calcium removing system |
| JP2007136409A (en) * | 2005-11-22 | 2007-06-07 | Sharp Corp | Water treatment method and water treatment apparatus |
| JP2007313445A (en) * | 2006-05-26 | 2007-12-06 | Nippon Rensui Co Ltd | Wastewater treatment method, wastewater treatment apparatus, and wastewater recovery system |
| CN102838199A (en) * | 2012-09-26 | 2012-12-26 | 河海大学 | Device and method for removing fluorine ions in groundwater |
| CN102838236A (en) * | 2012-09-26 | 2012-12-26 | 河海大学 | Equipment and method for removing manganese ions in underground water |
| JP2017018846A (en) * | 2015-07-07 | 2017-01-26 | 日本リファイン株式会社 | Water treatment method for anionic surfactant-containing water |
-
1992
- 1992-09-29 JP JP4259263A patent/JPH06106170A/en not_active Withdrawn
Cited By (8)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2005161224A (en) * | 2003-12-03 | 2005-06-23 | Fujita Corp | Calcium removing method and calcium removing system |
| JP4666905B2 (en) * | 2003-12-03 | 2011-04-06 | 株式会社フジタ | Calcium removal method and calcium removal system |
| JP2007136409A (en) * | 2005-11-22 | 2007-06-07 | Sharp Corp | Water treatment method and water treatment apparatus |
| JP4490904B2 (en) * | 2005-11-22 | 2010-06-30 | シャープ株式会社 | Water treatment equipment |
| JP2007313445A (en) * | 2006-05-26 | 2007-12-06 | Nippon Rensui Co Ltd | Wastewater treatment method, wastewater treatment apparatus, and wastewater recovery system |
| CN102838199A (en) * | 2012-09-26 | 2012-12-26 | 河海大学 | Device and method for removing fluorine ions in groundwater |
| CN102838236A (en) * | 2012-09-26 | 2012-12-26 | 河海大学 | Equipment and method for removing manganese ions in underground water |
| JP2017018846A (en) * | 2015-07-07 | 2017-01-26 | 日本リファイン株式会社 | Water treatment method for anionic surfactant-containing water |
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