JPH09253625A - Wastewater treatment method - Google Patents
Wastewater treatment methodInfo
- Publication number
- JPH09253625A JPH09253625A JP6641496A JP6641496A JPH09253625A JP H09253625 A JPH09253625 A JP H09253625A JP 6641496 A JP6641496 A JP 6641496A JP 6641496 A JP6641496 A JP 6641496A JP H09253625 A JPH09253625 A JP H09253625A
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- wastewater
- filter
- treated
- filtration
- 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
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- Separation Using Semi-Permeable Membranes (AREA)
- Water Treatment By Sorption (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は植物材料を吸着剤と
して使用する排水の処理方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a wastewater treatment method using a plant material as an adsorbent.
【０００２】[0002]
【従来の技術】従来、排水の処理方法としては、活性汚
泥法やその他の微生物学的処理法、濃縮・乾燥法等が知
られているが、いずれも処理に長時間を要する、多額の
設備量を必要とする、等の理由で必ずしも実用的、経済
的に有利な方法とは言えなかった。2. Description of the Related Art Conventionally, as a method for treating wastewater, an activated sludge method, other microbiological treatment methods, concentration / drying methods, etc. have been known. It was not always a practical or economically advantageous method because it required a large amount.
【０００３】[0003]
【発明が解決しようとする課題】そこで本発明は、短時
間で排水処理ができ、且つ多額の設備費を必要としない
排水処理方法を提供しようとするものである。SUMMARY OF THE INVENTION Therefore, the present invention is intended to provide a wastewater treatment method capable of treating wastewater in a short time and not requiring a large amount of equipment cost.
【０００４】[0004]
【課題を解決するための手段】上記の課題を解決するた
め、本発明は、処理すべき排水１００重量部と、平均粒
径１００ミクロン以下に破砕した植物性粉末１〜１０重
量部とを均一に混合し、この混合物を固体と液体とに分
離し、そして分離した液体を孔径５ミクロン以下のフィ
ルターにより濾過することを特徴とする排水の処理方法
を提供する。In order to solve the above problems, the present invention uniformly comprises 100 parts by weight of waste water to be treated and 1 to 10 parts by weight of vegetable powder crushed to an average particle size of 100 microns or less. The present invention provides a method for treating wastewater, which comprises mixing the mixture into a solid and a liquid and separating the separated liquid through a filter having a pore size of 5 microns or less.
【０００５】[0005]
【発明の実施の形態】本発明の方法により処理される排
水は、各種産業排水、家庭用排水、下水処理物からの排
水、し尿処理場からの排水、家畜し尿等、種々の排水の
処理のために使用することができ、かなり強い酸性又は
塩基水の排水も、そのまま又は水で希釈しただけで処理
するととができる。本発明の方法によれば、処理すべき
原排水をそのまま処理に付すこともできるが、排水の濃
度によっては、処理前に原排水をそれとおよそ同量まで
の水により希釈する場合もある。この希釈は吸着剤とし
ての植物性粉末と混合する前に行こともできるが、排水
と植物性粉末とを混合するための混合槽に希釈水を加え
ることによっても行うことができる。この希釈水として
は、本発明の方法による処理済水の一部を再循環して使
用するのが好ましい。BEST MODE FOR CARRYING OUT THE INVENTION The wastewater treated by the method of the present invention is used for the treatment of various industrial wastewater, domestic wastewater, wastewater from a sewage treatment product, wastewater from a human waste treatment plant, livestock human waste, etc. It can also be used for treating very strong acidic or basic water drainage, either neat or just diluted with water. According to the method of the present invention, the raw wastewater to be treated can be directly subjected to the treatment, but depending on the concentration of the wastewater, the raw wastewater may be diluted with approximately the same amount of water as that before the treatment. This dilution can be performed before mixing with the vegetable powder as the adsorbent, but can also be performed by adding the dilution water to the mixing tank for mixing the waste water and the vegetable powder. As this dilution water, it is preferable to recycle and use a part of the water treated by the method of the present invention.
【０００６】吸着剤としての植物性粉末は、処理すべき
排水中に含まれる種々のＣＯＤ又はＢＯＤ原因物質、臭
気発生源物質、着色物質、各種イオン性物質、例えば種
々の金属イオン、陰イオン、無機塩類等を吸着するもの
であればその由来を問わない。これらの植物性材料とし
ては、フスマ、例えば小麦フスマ、オカラ、オガクズ、
コーヒーカス、落葉、イネワラ、ムギワラ、野菜くず等
種々のものが挙げられる。しかしながら、高価でなく、
大量に安定して入手可能である等の実用的見地から、小
麦フスマ、オカラ、オガクズ等が特に好ましい。これら
は乾燥した状態で破砕して使用する。破砕のためには常
用の粉砕機を用いることができる。The vegetable powder as an adsorbent contains various COD or BOD-causing substances, odor generating substances, coloring substances and various ionic substances contained in the wastewater to be treated, such as various metal ions and anions. The origin is not limited as long as it can adsorb inorganic salts and the like. These plant materials include bran, such as wheat bran, okara, sawdust,
Various things such as coffee dregs, fallen leaves, rice straw, wheat straw, vegetable scraps and the like can be mentioned. However, it is not expensive,
Wheat bran, okara, sawdust and the like are particularly preferable from the practical viewpoint that they can be stably obtained in large quantities. These are crushed in a dry state before use. A commonly used crusher can be used for crushing.
【０００７】破砕後の平均粒径は１００ミクロン以下で
あり、好ましくは７５ミクロン以下、さらに好ましくは
５０ミクロン以下であり、例えば７５〜１５ミクロンで
ある。しかし、処理すべき排液の性質によってはさらに
微粒であってもよい。植物性粉末の種類は、処理すべき
排水に依存して選択するのが好ましい。例えばイオン性
物質を含有する排水の処理において該イオン性物質の除
去や酸性又は塩基性の中和のためには蛋白質に富む植物
性粉末、例えば小麦フスマ、オガクズ、オカラ等から製
造したものが好ましく、着色物質の吸着のためにはオガ
クズが好ましく、臭気発生原物質の除去のためにはオガ
クズ及びコーヒーカスが好ましく、またＣＯＤやＤＯＤ
の低下のためにはオガクズが好ましい。The average particle size after crushing is 100 microns or less, preferably 75 microns or less, more preferably 50 microns or less, for example, 75 to 15 microns. However, it may be finer depending on the nature of the effluent to be treated. The type of vegetable powder is preferably selected depending on the wastewater to be treated. For example, in the treatment of wastewater containing ionic substances, in order to remove the ionic substances and neutralize the acidity or basicity, protein-rich plant powders, such as wheat bran, sawdust, and okara, are preferably produced. , Sawdust for adsorbing coloring substances, sawdust and coffee dregs for removing odor-producing substances, and COD and DOD
Scraps are preferred for the reduction of.
【０００８】本発明の方法の第一の段階においては、例
えば処理すべき排液を混合槽に入れ、これに植物性粉末
吸着剤を投入し、全体を均一に混合する。この際、排液
は、その中に含まれる除去すべき物質の種類及び量によ
り異るが、水により希釈するのが好ましい。この希釈水
の量は通常、処理すべき排液の原液の量と同量までであ
る。原排液の希釈は混合槽に入れる前行ってもよく、あ
るいは混合槽に入れた後、それに希釈水を加えるか、又
はあらかじめ混合槽に希釈水を入れておき、それに処理
すべき原排液を入れてもよい。植物性粉末吸着剤の量
は、処理すべき排液、すなわち希釈を行わない場合には
原排液１００重量部、希釈を行う場合には希釈した後の
排液１００重量部に対して、１〜１０重量部であり、好
ましくは２〜３重量部、そして通常は２〜６重量部であ
る。In the first step of the method of the present invention, for example, the effluent to be treated is put into a mixing tank, and the vegetable powder adsorbent is added to the mixing tank to uniformly mix the whole. At this time, the drainage liquid is preferably diluted with water, although it depends on the type and amount of the substance contained therein to be removed. The amount of dilution water is usually up to the same amount as the stock solution of the effluent to be treated. The raw effluent may be diluted before it is put in the mixing tank, or after it is put in the mixing tank, the dilution water is added to it, or the dilution water is put in the mixing tank in advance, and the raw effluent to be treated therein. May be included. The amount of the vegetable powder adsorbent is 1 part with respect to the effluent to be treated, that is, 100 parts by weight of the original effluent when not diluted, and 100 parts by weight of the diluted effluent when diluted. -10 parts by weight, preferably 2-3 parts by weight, and usually 2-6 parts by weight.
【０００９】排液と植物性粉末との混合は、混合槽中で
撹拌装置、例えば回転式撹拌機により行うのが好まし
い。また、通気により撹拌することもできる。混合は常
温にて、十分に均一になるまで行う。混合の時間は撹拌
装置の種類やパワーにより異るが、通常１０分間程度で
よい。The mixing of the drainage liquid and the vegetable powder is preferably carried out in a mixing tank with a stirring device, for example, a rotary stirring machine. It is also possible to stir by aeration. Mix at room temperature until it is sufficiently homogeneous. The mixing time depends on the type and power of the stirrer, but is usually about 10 minutes.
【００１０】次に、得られた混合物を固体と液体に分離
する。この分離は、固・液分離のために通常用いられる
方法及び装置を用いて行うことができ、例えば遠心分離
又は濾過により行う。実用上の見地からは濾過により行
うのがよく、この場合通常の濾過機を用いることができ
る。フィルターの開孔は４０ミクロン以下が好ましく、
例えば４０〜２０ミクロン、例えば３７．５ミクロンで
ある。なお、例えば植物性粉末として３７．５ミクロン
より粒径の小さい吸着剤を使用した場合でも、排水との
混合により吸水膨潤し、また相互に凝集して大粒子とな
るので、３７．５ミクロン開孔のフィルターにより濾去
することが可能である。Next, the obtained mixture is separated into a solid and a liquid. This separation can be carried out by using a method and a device usually used for solid / liquid separation, for example, centrifugation or filtration. From a practical point of view, it is preferable to carry out filtration, and in this case, an ordinary filter can be used. The aperture of the filter is preferably 40 microns or less,
For example, 40 to 20 microns, for example 37.5 microns. Even if an adsorbent having a particle size smaller than 37.5 μm is used as the vegetable powder, for example, since it absorbs and swells when mixed with the waste water and agglomerates with each other to form large particles, the 37.5 μm open powder is used. It is possible to filter out with a filter with holes.
【００１１】この段階での混合液には、比較的多量の固
形分が含まれているので、混合槽１本当たりの混合液を
複数回、例えば２〜４回に分けて処理、例えば濾過する
のが好ましく、このためには、混合槽１本当たり複数
台、例えば２〜４台の濾過機を用意するのが好ましい。Since the mixed liquid at this stage contains a relatively large amount of solid content, the mixed liquid per one mixing tank is treated plural times, for example, 2 to 4 times, for example, filtered. For this purpose, it is preferable to prepare a plurality of, for example, 2 to 4 filters per one mixing tank.
【００１２】次に、濾液を、１回又は複数回、例えば２
〜３回濾過することによりさらに清澄化する。この場
合、フィルターの孔径は濾過を反復するごとに小さくす
る。例えば、前記の混合液を固・液分離したすぐ後の濾
過においては、孔径５〜２ミクロンのフィルターを使用
し、次に１〜２ミクロンの孔径のフィルターを使用し、
最後に０．５〜０．１ミクロンの孔径のフィルターを使
用する。例えば、前記の混合液の固・液分離を孔径３
７．５ミクロンのフィルターを用いて行った後、約３ミ
クロン孔径のフィルターで濾過し、次にその濾液を１．
２ミクロン孔径のフィルターで濾過し、最後に０．２２
ミクロン孔径のフィルターにより濾過する。この濾過に
より、大腸菌その他の細菌はほとんど除去される。The filtrate is then treated once or several times, for example 2 times.
Further clarification by filtration ~ 3 times. In this case, the pore size of the filter is reduced with each repetition of filtration. For example, in the filtration immediately after solid-liquid separation of the mixed solution, a filter having a pore size of 5 to 2 microns is used, and then a filter having a pore size of 1 to 2 microns is used.
Finally a filter with a pore size of 0.5-0.1 micron is used. For example, the solid / liquid separation of the above-mentioned mixed liquid is performed with a pore size of 3
After working with a 7.5 micron filter, it is filtered through a filter with a pore size of about 3 microns and then the filtrate is 1.
Filter through a 2 micron pore size filter and finally 0.22
Filter through a micron pore size filter. By this filtration, most of Escherichia coli and other bacteria are removed.
【００１３】上記の各段階の濾過は、通常の濾過機及び
濾過膜を用いて行うことができる。各濾過機の間には、
濾液を一時的に貯留するための待ち槽を設けるのが好ま
しく、この待ち槽の容量は、混合槽と同等か又はそれよ
り小さくてもよい。最初の待ち槽、すなわち、混合液の
固液濾過を行った直後の待ち槽には撹拌機及び水を供給
する配管を設けることが好ましい。また、最終濾過（除
菌）の後、処理済水は貯留槽に貯えるのが好ましい。混
合槽及び第一の待ち槽等に希釈水として供給する水はこ
の貯留槽から送水するのが便利である。The filtration in each of the above steps can be carried out using a usual filter and a filtration membrane. Between each filter,
It is preferable to provide a waiting tank for temporarily storing the filtrate, and the capacity of the waiting tank may be equal to or smaller than that of the mixing tank. A stirrer and a pipe for supplying water are preferably provided in the first waiting tank, that is, the waiting tank immediately after the solid-liquid filtration of the mixed liquid. Further, it is preferable to store the treated water in a storage tank after the final filtration (sterilization). It is convenient to send water supplied as dilution water to the mixing tank, the first waiting tank, etc. from this storage tank.
【００１４】次に、本発明を、図面に基いてさらに具体
的に説明する。図１は本発明の方法を実施するための装
置の略図である。撹拌機３を有する混合槽２に、処理す
べき原排液１を入れ、所望により配管４から希釈水を加
え、それに植物性粉末を添加して撹拌機３により全体を
均一に混合する。次にこの混合液をポンプ（Ｐ1 ）５に
より濾過機Ｆａ〜Ｆｄのいずれか１つ例えばＦａに圧送
し、濾過により固液分離する。この濾過機は例えば孔径
３７．５ミクロンの濾過膜を有する。濾過機Ｆａの容量
が満たされた時、又は目詰りしたとき、Ｆａへの圧送を
停止し、他の濾過機、例えばＦｂに切り替えて混合液を
圧送し、濾過する。こうして得られた濾過は、配管７を
通して最初の待ち槽９に入れる。Next, the present invention will be described more specifically with reference to the drawings. FIG. 1 is a schematic diagram of an apparatus for carrying out the method of the present invention. The raw effluent 1 to be treated is put in a mixing tank 2 having a stirrer 3, diluted water is added from a pipe 4 if desired, and vegetable powder is added thereto, and the whole is uniformly mixed by the stirrer 3. Next, this mixed liquid is pressure-fed by a pump (P 1 ) 5 to any one of the filters Fa to Fd, for example, Fa, and solid-liquid separation is performed by filtration. This filter has, for example, a filter membrane with a pore size of 37.5 microns. When the capacity of the filter Fa is filled or when it is clogged, the pressure feed to Fa is stopped, and the filter is switched to another filter, for example, Fb, and the mixed liquid is pressure fed and filtered. The thus obtained filtration is put into the first waiting tank 9 through the pipe 7.
【００１５】待ち槽９には、必要であれば配管１１から
希釈水を注入することにより濾液の希釈を行う。次に、
この濾過をポンプ（Ｐ2 ）１２により濾過機（Ｆ1 ）１
３に圧送し、残存する微粒子の濾去を行う。濾過機（Ｆ
1 ）１３は、例えば孔径３ミクロンの濾過膜を有する。
次に濾液は配管１４を通して待ち槽１５に入れた後、ポ
ンプ（Ｐ3 ）１６により次の濾過機（Ｆ2 ）１７に圧送
する。濾過機（Ｆ2 ）１７は例えば孔径１．２ミクロン
の濾過膜を有する。次に濾液は配管１８により待ち槽１
９に送り、さらに、ポンプ（Ｐ4 ）２０により濾過機
（Ｆ3 ）２１に圧送して除菌濾過を行う。濾過機
（Ｆ3 ）２１は孔径０．２２ミクロンの濾過膜を有し、
除菌を行うことができる。処理を終えた水は貯留槽２２
に貯留され、その一部は配管２３から配管４及び１１を
通して、本発明の方法における希釈水として再循環して
利用することができ、他は種々の目的で再利用すること
ができる。If necessary, dilution water is injected into the waiting tank 9 through a pipe 11 to dilute the filtrate. next,
This filtration is carried out by a pump (P 2 ) 12 and a filter (F 1 ) 1
It is pressure-fed to 3 and the remaining fine particles are filtered off. Filter (F
1 ) 13 has, for example, a filtration membrane having a pore size of 3 microns.
Next, the filtrate is put into a waiting tank 15 through a pipe 14 and then pumped to a next filter (F 2 ) 17 by a pump (P 3 ) 16. The filter (F 2 ) 17 has, for example, a filter membrane having a pore size of 1.2 microns. Next, the filtrate is supplied to the waiting tank 1 through the pipe 18.
9, and further pumped by a pump (P 4 ) 20 to a filter (F 3 ) 21 for sterilization filtration. The filter (F 3 ) 21 has a filter membrane with a pore size of 0.22 micron,
Sterilization can be performed. The treated water is stored in the storage tank 22.
Part of which can be reused by recirculating it from the pipe 23 through the pipes 4 and 11 as the dilution water in the method of the present invention, and the other for various purposes.
【００１６】[0016]
【発明の効果】本発明により、現状では活性汚泥法処理
によって基準に適合し得なかった各種の産業排水、家庭
用排水、下水処理場排水、し尿処理場排水、家畜し尿処
場排水を基準内処理し、同時に臭気発生源物質、着色物
質、各種イオン性物質、金属イオン、陰イオン、無機塩
類も吸着して清澄化し現状ＢＯＤ，ＣＯＤも基準内処理
が極めて安価に処理することができるようになった。従
って本発明は水環境に対する貢献度は多大である。Industrial Applicability According to the present invention, various industrial wastewater, domestic wastewater, sewage treatment plant wastewater, human waste treatment plant drainage, and livestock human waste treatment plant drainage that do not currently meet the standards by the activated sludge method treatment are within the standards. At the same time, the odor generating substances, coloring substances, various ionic substances, metal ions, anions, and inorganic salts are also adsorbed and clarified so that BOD and COD can be treated at a very low cost within the standard treatment. became. Therefore, the present invention makes a great contribution to the water environment.
【００１７】[0017]
【実施例】本発明を実施例によりさらに具体的に説明す
る。実施例１． 図１に模式的に示す装置を用いて、カツオ節
製造工場の排水を処理した。混合槽２に排液を入れ、排
液１０００Kg当り約５Kgの植物性粉末（オガクズ５０
％、コーヒーカス５０％の重量比の混合物を粒径７５ミ
クロンに粉砕したもの）を入れ、高速撹拌機３により約
１０分間高速撹拌して均一に混合した。次に排液に対し
て２倍量の地下水を混合槽２に加えて撹拌することによ
り希釈した。次に、この混合液をポンプＰ1 （５）によ
り濾過機６に圧送し、この濾点機において孔径３７．５
ミクロンの濾過膜に通して濾過した。この濾液を待ち槽
９に入れ、これにもとの排液と同量の地下水を加えて混
合し、希釈を行った。EXAMPLES The present invention will be described more specifically with reference to examples. Embodiment 1 FIG. Wastewater from a bonito flakes manufacturing plant was treated using the apparatus schematically shown in FIG. Drainage is put into the mixing tank 2 and about 5 kg of plant powder (50% of sawdust) per 1000 kg of drainage.
%, 50% by weight of coffee grounds was pulverized to a particle size of 75 microns), and the mixture was uniformly stirred by high-speed stirring for about 10 minutes by a high-speed stirrer 3. Next, twice the amount of groundwater to the drainage was added to the mixing tank 2 and stirred to dilute. Next, this mixed solution is pressure-fed to the filter 6 by the pump P 1 (5), and the pore size is 37.5 in this filter point machine.
Filter through a micron filter membrane. This filtrate was put in the waiting tank 9, and the same amount of groundwater as the original drainage was added to this and mixed to dilute.
【００１８】次に、待ち槽９の液をポンプＰ2 （１２）
により濾過機Ｆ1 （１３）に圧送した。濾過機１３は孔
径３ミクロンの濾過膜を有する。この濾液を一旦待ち槽
１５に入れた後、ポンプＰ3 （１６）により濾過機１７
に送り、濾過を行った。この濾過機は孔径１．２ミクロ
ンの濾過膜を有する。この濾液を待ち槽１９に入れた
後、ポンプＰ4 （２０）により濾過機Ｆ3 （２１）に送
る。この濾過機は孔径０．２２ミクロンの濾過膜を有
し、細菌を濾去することができる。次に、無菌濾過した
液を貯留槽２２に入れた。この最終処理された液は、種
々の用途に再理用することができる か、混合槽２及び
待ち槽９への割り水として使用することができる。Next, the liquid in the waiting tank 9 is pumped by the pump P 2 (12).
And pressure fed to the filter F 1 (13). The filter 13 has a filter membrane with a pore size of 3 microns. This filtrate was once put in the waiting tank 15 and then filtered by a pump 17 using a pump P 3 (16).
And filtered. This filter has a filtration membrane with a pore size of 1.2 microns. After putting this filtrate in the waiting tank 19, it is sent to the filter F 3 (21) by the pump P 4 (20). This filter has a 0.22 micron pore size filtration membrane and is capable of filtering out bacteria. Next, the aseptically filtered liquid was placed in the storage tank 22. This finally treated liquid can be reused for various purposes, or can be used as water for dividing into the mixing tank 2 and the waiting tank 9.
【００１９】上記の処理により、ＢＯＤ：２９，０００
ppm 及びＣＯＤ：２０，０００ppmを有する排水から、
ＢＯＤ：６２ppm 及びＣＯＤ：９５ppm を有する透明な
処理済水を得た。全処理時間は５５分間であった。By the above processing, BOD: 29,000
From wastewater having ppm and COD: 20,000 ppm,
A clear treated water having a BOD of 62 ppm and a COD of 95 ppm was obtained. The total treatment time was 55 minutes.
【００２０】実施例２．カツオ節製造工業の別の排水を
実施例１に記載したようにして処理した。処理前の排水
のＢＯＤが２４４０mg／Ｌ、ＣＯＤが１９５０mg／Ｌで
あり、透明な処理済水のＢＯＤが４．２mg／Ｌ、ＣＯＤ
が４．８mg／Ｌであり、合計処理時間は７０時間であっ
た。 Embodiment 2 FIG . Another effluent from the skipjack mill industry was treated as described in Example 1. BOD of wastewater before treatment is 2440 mg / L, COD is 1950 mg / L, BOD of transparent treated water is 4.2 mg / L, COD
Was 4.8 mg / L and the total treatment time was 70 hours.
【００２１】実施例３．火力発電所の水管路に付着した
ムラサキ貝を除去し、野積みしている間に生じた腐敗水
を、実施例１と同様に悪臭の除去を目的として処理し
た。処理前の排水の臭気成分の含量は硫化水素４００pp
m 、メチルメルカプタン１２０ppm 、プロピレン６０pp
m 及びエチルメルカプタン３ppm であり、処理後におい
ては、これらの物質は検出されず臭気もなかった。な
お、測定には北川式ガス検知管を用いた。また、処理前
のＣＯＤが８，９００mg／Ｌであり処理後５．５mg／Ｌ
に低下し、ｓｓは処理前６，８００mg／Ｌであり処理後
は５．０mg／Ｌであった。処理に要した時間は７０分間
であった。 Embodiment 3 FIG . The mussels adhering to the water pipes of the thermal power plant were removed, and the spoiled water generated during field loading was treated in the same manner as in Example 1 for the purpose of removing malodor. The content of odorous components in the wastewater before treatment is 400 pp of hydrogen sulfide.
m, methyl mercaptan 120ppm, propylene 60pp
m 3 and ethyl mercaptan were 3 ppm, and these substances were not detected and had no odor after the treatment. A Kitagawa gas detector tube was used for the measurement. The COD before treatment was 8,900 mg / L, and the COD after treatment was 5.5 mg / L.
The ss was 6,800 mg / L before the treatment and 5.0 mg / L after the treatment. The time required for the treatment was 70 minutes.
【００２２】実施例４．染色工業の排水を実施例１に記
載したようにして処理した。但し、植物性吸着剤粉末と
してはオガクズのみから作ったものを使用した。処理前
の排水のＣＯＤ及びＰＯＰは約４０〜８０mg／Ｌであ
り、処理後、ＢＯＤが１．２mg／Ｌ、ＣＯＤが３．７mg
／Ｌに低下した。処理時間は６１分間であった。 Example 4. Dyeing industry effluent was treated as described in Example 1. However, as the vegetable adsorbent powder, a powder made only of sawdust was used. The COD and POP of the wastewater before treatment are about 40 to 80 mg / L, and the BOD after treatment is 1.2 mg / L and the COD is 3.7 mg.
/ L. The processing time was 61 minutes.
【００２３】実施例５．染色工業の排水を実施例４に記
載したのと同様にして処理した。処理前の排水のＢＯＤ
及びＣＯＤは約６００mg／Ｌであった。処理後の水のＢ
ＯＤは２．９mg／Ｌであり、ＣＯＤは７．０mg／Ｌであ
った。処理時間は６３分間であった。 Example 5. Dyeing industry effluent was treated as described in Example 4. BOD of wastewater before treatment
And COD was about 600 mg / L. B of treated water
The OD was 2.9 mg / L and the COD was 7.0 mg / L. The processing time was 63 minutes.
【００２４】実施例６．管理型産業廃棄物最終処分場地
下癈棄物処理水を、実施例４に記載したのと同様にして
処理した。処理前の排水のＮａは１３００mg／Ｌ、Ｃｌ
は１７５０mg／Ｌであり、処理後においてはＮａは２７
mg／Ｌ、Ｃｌは３８mg／Ｌとなった。処理時間は３５分
間であった。この処理は３ミクロン濾過までの処理であ
った。 Example 6. Controlled industrial waste final disposal site Underground waste treatment water was treated in the same manner as described in Example 4. Na in the wastewater before treatment is 1300 mg / L, Cl
Is 1750 mg / L, and Na is 27 after the treatment.
mg / L and Cl became 38 mg / L. The processing time was 35 minutes. This treatment was up to 3 micron filtration.
【図１】図１は、本発明の方法を実施するための装置の
模式図である。FIG. 1 is a schematic view of an apparatus for carrying out the method of the present invention.
１…排水 ２…混合槽 ５，１２，１６，２０…ポンプ ６，１３，１７，２１…濾過機 ９，１５，１９…待ち槽 1 ... Drainage 2 ... Mixing tank 5,12,16,20 ... Pump 6,13,17,21 ... Filtration machine 9,15,19 ... Wait tank
Claims (6)
径１００ミクロン以下に破砕した植物性粉末１〜１０重
量部とを均一に混合し、この混合物を固体と液体とに分
離し、そして分離した液体を孔径５ミクロン以下のフィ
ルターにより濾過することを特徴とする排水の処理方
法。1. 100 parts by weight of waste water to be treated and 1 to 10 parts by weight of plant powder crushed to an average particle size of 100 microns or less are uniformly mixed, and this mixture is separated into a solid and a liquid, and A method for treating wastewater, which comprises filtering the separated liquid with a filter having a pore size of 5 microns or less.
クズ、コーヒーカス、米糠、落葉、イネワラ、ムギワラ
又は野菜くずである、請求項１に記載の方法。2. The method according to claim 1, wherein the vegetable powder is bran, okara, sawdust, coffee dregs, rice bran, deciduous leaves, rice straw, wheat straw or vegetable waste.
ヒーカス又はオガクズでありその粒径が７５〜１５ミク
ロンである請求項１に記載の方法。3. The method according to claim 1, wherein the vegetable powder is bran, okara, coffee grounds or sawdust, and the particle size is 75 to 15 microns.
い、濾過時の孔形が４０ミクロン以下である、請求項１
に記載の方法。4. The separation of the solid and the liquid is performed by filtration, and the pore shape at the time of filtration is 40 μm or less.
The method described in.
い、濾過を反復するごとにフィルターの孔径を小さくす
る、請求項１に記載の方法。5. The method according to claim 1, wherein the liquid after the solid-liquid separation is filtered a plurality of times, and the pore size of the filter is reduced each time the filtration is repeated.
として循環使用する、請求項１に記載の方法。6. The method according to claim 1, wherein the treated water is recycled as dilution water of the wastewater to be treated.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6641496A JPH09253625A (en) | 1996-03-22 | 1996-03-22 | Wastewater treatment method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP6641496A JPH09253625A (en) | 1996-03-22 | 1996-03-22 | Wastewater treatment method |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH09253625A true JPH09253625A (en) | 1997-09-30 |
Family
ID=13315122
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP6641496A Pending JPH09253625A (en) | 1996-03-22 | 1996-03-22 | Wastewater treatment method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH09253625A (en) |
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR20010083023A (en) * | 2000-04-01 | 2001-08-31 | 차상태 | System of filtering wastewater and method thereof |
| JP2002537110A (en) * | 1999-02-24 | 2002-11-05 | ビジィアム バイオサイエンシズ リミテッド | Novel agropolymer used for purification of contaminated water or polluted water containing metal or ions, and method for producing the agropolymer |
| JP2011194385A (en) * | 2010-03-24 | 2011-10-06 | Sony Corp | Cation exchanger and method for removing heavy metal ion in wastewater |
| JP2012066963A (en) * | 2010-09-22 | 2012-04-05 | Noritake Co Ltd | Method for producing porous ceramic base material and multistage filter |
-
1996
- 1996-03-22 JP JP6641496A patent/JPH09253625A/en active Pending
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002537110A (en) * | 1999-02-24 | 2002-11-05 | ビジィアム バイオサイエンシズ リミテッド | Novel agropolymer used for purification of contaminated water or polluted water containing metal or ions, and method for producing the agropolymer |
| JP4822586B2 (en) * | 1999-02-24 | 2011-11-24 | ビジャム バイオサイエンシズ プライヴェート リミテッド | Method for producing agropolymer and method for using the agropolymer for purification of contaminated water or contaminated water containing metal or ions |
| KR20010083023A (en) * | 2000-04-01 | 2001-08-31 | 차상태 | System of filtering wastewater and method thereof |
| JP2011194385A (en) * | 2010-03-24 | 2011-10-06 | Sony Corp | Cation exchanger and method for removing heavy metal ion in wastewater |
| JP2012066963A (en) * | 2010-09-22 | 2012-04-05 | Noritake Co Ltd | Method for producing porous ceramic base material and multistage filter |
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