JP2002263660A - Facility for purifying water - Google Patents
Facility for purifying waterInfo
- Publication number
- JP2002263660A JP2002263660A JP2001064293A JP2001064293A JP2002263660A JP 2002263660 A JP2002263660 A JP 2002263660A JP 2001064293 A JP2001064293 A JP 2001064293A JP 2001064293 A JP2001064293 A JP 2001064293A JP 2002263660 A JP2002263660 A JP 2002263660A
- Authority
- JP
- Japan
- Prior art keywords
- water
- filtration
- mixing
- sedimentation
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
Landscapes
- Separation Of Suspended Particles By Flocculating Agents (AREA)
- Filtration Of Liquid (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、無機凝集剤を混合
後に有機高分子凝集剤（ポリマー）を混合し凝集沈殿処
理を行う凝集沈殿処理装置と、凝集沈殿処理水について
砂ろ過処理を行う砂ろ過装置を有する浄水処理装置に関
する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a coagulation / sedimentation treatment apparatus for mixing an inorganic coagulant and then mixing an organic polymer coagulant (polymer) for coagulation / sedimentation treatment, and a sand for performing sand filtration treatment on coagulation / sedimentation treatment water The present invention relates to a water purification device having a filtration device.
【０００２】[0002]
【従来の技術】従来より河川水、湖沼水等の表流水を原
水とする浄水処理において、凝集沈殿処理と砂ろ過を組
み合わせた処理が広く採用されている。2. Description of the Related Art Conventionally, in water purification treatment using surface water such as river water, lake water, or the like as raw water, treatment that combines coagulation sedimentation treatment and sand filtration has been widely used.
【０００３】この凝集沈殿処理では、アルミ系や鉄系の
無機凝集剤が利用されているが、これら無機凝集剤に有
機高分子凝集剤を併用する場合も多い。これは、ポリマ
ーを利用することで、微細な無機凝集剤フロックや懸濁
物質を容易に粗大化でき、沈降速度を上昇して良好な沈
殿上澄み液を安定して得ることができるからである。In this coagulation-precipitation treatment, an aluminum-based or iron-based inorganic coagulant is used. In many cases, an organic polymer coagulant is used in combination with these inorganic coagulants. This is because, by using a polymer, a fine inorganic flocculant floc or a suspended substance can be easily coarsened, a sedimentation speed can be increased, and a good sedimentation supernatant can be stably obtained.
【０００４】そこで、良好なフロックが形成されるよう
に凝集条件を決定している。通常の場合、ポリマー添加
後の急速撹拌強度をＧ値で３００ｓｅｃ−１（以下ｓ
−１と記す）未満、急速撹拌時間を５分未満になるよう
にしている。これによって、フロックの最大成長径は１
０ｍｍ前後あるいはそれ以上に達し、沈殿池におけるフ
ロック沈降速度が上昇し、沈殿上澄み液の水質を向上す
ることができる。[0004] Therefore, the coagulation conditions are determined so that a good floc is formed. In the normal case, the rapid stirring intensity after adding the polymer is 300 sec −1 (hereinafter referred to as s) in G value.
-1 ) and the rapid stirring time is less than 5 minutes. Thus, the maximum growth diameter of the flock is 1
When it reaches about 0 mm or more, the floc sedimentation velocity in the sedimentation basin increases, and the water quality of the sedimentation supernatant can be improved.
【０００５】[0005]
【発明が解決しようとする課題】ところが、フロックの
成長を優先させて、撹拌強度を３００ｓ−１未満とした
り、急速撹拌時間を５分未満になるようすると、沈殿池
でのフロックの除去性は向上し、沈殿上澄み水の濁度や
ＳＳ（懸濁物質濃度）といった定量的指標でみるとその
絶対値は小さくなる。しかし、このような凝集では微小
な粒子がフロックに取り込まれず、これがろ過池に供給
されてろ過抵抗が増加しやすいという問題があった。そ
して、ろ過抵抗が上昇しやすいと、逆洗頻度が増加し逆
洗が遅れるとブレークスルーが発生し、処理水質が悪化
してしまうという問題があった。However, if the stirring intensity is set to less than 300 s -1 or the rapid stirring time is set to less than 5 minutes by giving priority to the growth of flocs, the removability of flocs in the sedimentation basin is reduced. The absolute value decreases when viewed from quantitative indices such as turbidity of the supernatant supernatant water and SS (concentration of suspended solids). However, in such agglomeration, there is a problem that fine particles are not taken into the flocs, and are supplied to the filtration pond to increase the filtration resistance. When the filtration resistance is easily increased, the frequency of the backwash increases, and if the backwash is delayed, a breakthrough occurs and the quality of the treated water is deteriorated.
【０００６】一方、ポリマー添加後の急速撹拌の撹拌強
度を、Ｇ値で３００ｓ−１以上とし、５分以上行うと、
撹拌強度が比較的強いことにより、フロックの最大成長
径が数ｍｍにとどまる。このため、フロックの沈降速度
は、無機単独の場合に比べそれほど増加せず、沈殿処理
水の濁度も攪拌強度を弱くした場合のようによくならな
い。このため、ポリマーを添加したにもかかわらず沈殿
池を小さくできないという問題があった。On the other hand, when the stirring intensity of the rapid stirring after the addition of the polymer is set to a G value of 300 s −1 or more, when the stirring is performed for 5 minutes or more,
Due to the relatively high stirring intensity, the maximum growth diameter of the flocks is limited to several mm. For this reason, the sedimentation speed of the floc does not increase so much as compared with the case of the inorganic substance alone, and the turbidity of the sedimentation treatment water is not as good as when the stirring intensity is weakened. For this reason, there was a problem that the size of the sedimentation basin could not be reduced despite the addition of the polymer.
【０００７】本発明は上記課題に鑑みなされたものであ
り、最終的な処理水水質を向上することができる浄水装
置を提供することを目的とする。The present invention has been made in view of the above problems, and has as its object to provide a water purification device capable of improving the quality of final treated water.
【０００８】[0008]
【課題を解決するための手段】本発明は、無機凝集剤を
混合後に有機高分子凝集剤を混合し凝集沈殿処理を行う
凝集沈殿処理装置と、凝集沈殿処理水について砂ろ過処
理を行う砂ろ過装置を有する浄水処理装置であって、前
記有機高分子凝集剤の混和を撹拌強度Ｇ値で３００〜１
０００ｓｅｃ−１で５分以上行うとともに、前記砂ろ過
装置の前段で繊維をろ材に用いた繊維ろ過装置による粗
ろ過処理を行うことを特徴とする。SUMMARY OF THE INVENTION The present invention relates to a coagulation / sedimentation treatment apparatus for mixing an inorganic coagulant, mixing an organic polymer coagulant and performing coagulation / sedimentation treatment, and a sand filtration apparatus for performing sand filtration on coagulation / sedimentation treatment water. A water purification treatment device having a device, wherein the mixing of the organic polymer flocculant is 300 to 1 with stirring intensity G value.
000 sec -1 for 5 minutes or more, and a rough filtration treatment by a fiber filtration device using a fiber as a filter medium is performed in a preceding stage of the sand filtration device.
【０００９】このように、比較的強い攪拌で、有機高分
子凝集剤を混合することで、有機高分子凝集剤により、
微細な懸濁物質を細くすることができる。一方、このよ
うな強い攪拌を行うと、フロック径が十分大きくなら
ず、微細フロックが沈殿池より流出する可能性が高い
が、これは繊維ろ過で除去することができる。繊維ろ過
器はろ過速度を大きくとれるため、装置の全体としての
大きさ（浄水装置全体）を小さくできる。そして、繊維
ろ過器の処理水には、微細懸濁物質が非常に少ないた
め、砂ろ過供給水濁度が安定し、砂ろ過装置におけるろ
過抵抗の低減が図れる。As described above, by mixing the organic polymer flocculant with relatively strong stirring,
Fine suspended substances can be thinned. On the other hand, when such strong stirring is performed, the floc diameter does not become sufficiently large, and there is a high possibility that the fine floc flows out of the sedimentation basin. However, this can be removed by fiber filtration. Since the filtration speed of the fiber filter can be increased, the overall size of the apparatus (the entire water purification apparatus) can be reduced. And, since there is very little fine suspended substance in the treated water of the fiber filter, the turbidity of the sand filtration supply water is stabilized, and the filtration resistance in the sand filtration device can be reduced.
【００１０】また、前記凝集沈殿装置の表面負荷率（単
位時間の処理水量／沈殿池の有効断面積）が３．５ｍ／
時以上、前記繊維ろ過装置のろ過速度が１０ｍ／時以上
であることが好適である。Further, the surface load ratio (the amount of treated water per unit time / the effective sectional area of the sedimentation basin) of the coagulation settling apparatus is 3.5 m /
It is preferable that the filtration speed of the fiber filtration device be 10 m / hour or more.
【００１１】また、前記繊維ろ過装置のろ材が長さ５０
ｃｍ〜３００ｃｍの長繊維束であることが好適である。Further, the filter medium of the fiber filtration device has a length of 50
It is preferably a long fiber bundle of cm to 300 cm.
【００１２】[0012]
【発明の実施の形態】以下、本発明の実施形態につい
て、図面に基づいて説明する。Embodiments of the present invention will be described below with reference to the drawings.
【００１３】河川水、湖沼水等の表流水からなる原水
は、無機混和池１０に導入される。この無機混和池１０
には、攪拌翼１２ａと、これを回転させるモータ１２ｂ
からなる攪拌機１２が配置されている。また、この無機
混和池１０には、無機凝集剤タンク１４内の無機凝集剤
がポンプ１６によって供給される。無機凝集剤として
は、例えばＰＡＣ（ポリ塩化アルミニウム：Ａｌ２Ｏ３
１０％含有）が利用される。なお、この無機混和池１０
の急速攪拌強度は通常３００ｓ−１未満、滞留時間は５
分未満であるが、これに限定されない。Raw water consisting of surface water such as river water and lake water is introduced into the inorganic mixing pond 10. This inorganic mixing pond 10
Includes a stirring blade 12a and a motor 12b for rotating the stirring blade 12a.
Is disposed. The inorganic coagulant 10 is supplied with an inorganic coagulant in an inorganic coagulant tank 14 by a pump 16. As the inorganic flocculant, for example, PAC (polyaluminum chloride: Al 2 O 3)
10%). In addition, this inorganic mixing pond 10
Has a rapid stirring intensity of usually less than 300 s -1 and a residence time of 5
Minutes, but not limited to.
【００１４】次に、無機凝集剤が混合された水は、高分
子混和池１８に導入される。この高分子混和池１８に
は、攪拌翼２０ａと、これを回転させるモータ２０ｂか
らなる攪拌機２０が配置されており、また高分子凝集剤
タンク２２内の高分子凝集剤ががポンプ２４によって供
給される。高分子凝集剤としては、例えばノニオン性ア
クリルアミドポリマーが利用される。また、アニオン性
アクリルアミドポリマーが好適な場合もあるが、これら
に限定されるものではない。この高分子混和池１８の急
速攪拌強度は３００ｓ−１以上、滞留時間は５分以上に
設定されている。Next, the water mixed with the inorganic coagulant is introduced into the polymer mixing pond 18. A stirrer 20 including a stirring blade 20 a and a motor 20 b for rotating the stirring blade 20 a is disposed in the polymer mixing pond 18. The polymer flocculant in the polymer flocculant tank 22 is supplied by a pump 24. You. As the polymer flocculant, for example, a nonionic acrylamide polymer is used. In some cases, an anionic acrylamide polymer is suitable, but is not limited thereto. The rapid stirring strength of the polymer mixing pond 18 is set to 300 s -1 or more, and the residence time is set to 5 minutes or more.
【００１５】高分子混和池１８からの無機凝集剤および
高分子凝集剤が混合された水は、凝集池２６に導入され
る。この凝集池２６には横軸パドル式の緩速攪拌機２８
が設けられており、ここで緩速攪拌されフロックの粗大
化が図られる。The water mixed with the inorganic coagulant and the polymer coagulant from the polymer mixing pond 18 is introduced into the coagulation pond 26. The coagulation pond 26 has a horizontal paddle type slow stirrer 28
Is provided, and the floc is agitated at a low speed to increase the floc size.
【００１６】そして、無機凝集剤および高分子凝集剤に
よりフロック形成された水が沈殿池３０に導入され、こ
こで固形物が沈殿される。この沈殿池３０で沈殿された
固形物は汚泥として系外に排除され、上澄み水は繊維ろ
過器３２に導入される。Then, water flocculated by the inorganic flocculant and the polymer flocculant is introduced into the sedimentation basin 30, where solids are precipitated. The solids precipitated in the sedimentation basin 30 are removed as sludge outside the system, and the supernatant water is introduced into the fiber filter 32.
【００１７】この繊維ろ過器３２は、特公平５−１２０
０２号公報、特公平５−１１４８２号公報、特許第２７
９９３７６号公報などに記載されている長繊維束を利用
したものが好適である。この繊維ろ過器３２では、ろ過
塔の底部近傍に支持体を設け、この上方に長さ５０ｃｍ
〜３００ｃｍの長繊維束の下端を固定するとともに、上
端を自由端とする。そして、この長繊維束をろ過塔内に
ほぼ直立状態を維持するように充填し、ろ過体を形成す
る。そして、ろ過塔内に下降流で水を通過させてろ過体
により懸濁物質を捕捉除去する。このような繊維ろ過器
３２は、比較的空隙率が高く、砂ろ過池などに比べろ過
速度を十分大きくとれ、砂ろ過池に流入する水について
の粗ろ過が行える。すなわち、砂ろ過において、ろ過抵
抗上昇の原因となる微細なフロックを効果的に除去する
ことができる。なお、長繊維束の場合、このようなろ過
の際にその長さが上述のように５０ｃｍ〜３００ｃｍが
好適である。The fiber filter 32 has a structure of Japanese Patent Publication No. 5-120.
No. 02, Japanese Patent Publication No. 5-11482, Patent No. 27
Those using long fiber bundles described in, for example, Japanese Patent No. 99376 are preferable. In the fiber filter 32, a support is provided near the bottom of the filtration tower, and a length of 50 cm is provided above the support.
The lower end of the long fiber bundle of ~ 300 cm is fixed and the upper end is a free end. Then, the long fiber bundle is filled in the filtration tower so as to maintain a substantially upright state, thereby forming a filter. Then, water is passed through the filtration tower in a downward flow, and the suspended solids are captured and removed by the filter. Such a fiber filter 32 has a relatively high porosity, a sufficiently high filtration speed as compared with a sand filter or the like, and can perform coarse filtration of water flowing into the sand filter. That is, in sand filtration, fine flocs which cause an increase in filtration resistance can be effectively removed. In addition, in the case of a long fiber bundle, the length thereof is preferably 50 cm to 300 cm during the filtration as described above.
【００１８】この繊維ろ過器３２のろ過処理水は、次に
砂ろ過池３４に供給され、残留する懸濁物質がろ過処理
される。この砂ろ過池３４は、例えばアンスラサイト、
ケイ砂の二層で形成されており、比較的精密なろ過を行
う。これによって、水道水として配水できる水質のろ過
処理水が安定して得られる。The filtered water from the fiber filter 32 is then supplied to a sand filtration pond 34 where the remaining suspended solids are filtered. The sand filtration pond 34 includes, for example, anthracite,
It is formed of two layers of silica sand and performs relatively precise filtration. As a result, filtered water having a quality that can be distributed as tap water can be stably obtained.
【００１９】ろ過処理水は、処理水タンク３６に貯留さ
れ、消毒された後配水される。また、処理水タンク３６
内の処理水は、逆洗ポンプ３８によって、砂ろ過池３
４、繊維ろ過器３２の底部に供給できるようになってお
り、これによって砂ろ過池３４、繊維ろ過器３２を逆洗
できる。また、砂ろ過池３４、繊維ろ過器３２の底部に
はブロア４０からの空気も供給できるようになってお
り、これによって空気逆洗も行われる。The filtered water is stored in a treated water tank 36, and disinfected before being distributed. The treated water tank 36
The treated water in the sand filter pond 3
4. It can be supplied to the bottom of the fiber filter 32, so that the sand filter 34 and the fiber filter 32 can be backwashed. Further, the air from the blower 40 can be supplied to the bottoms of the sand filtration pond 34 and the fiber filter 32, whereby the air is backwashed.
【００２０】このような浄水装置において、沈殿池３０
からの沈殿処理水に微細なフロックが含まれても、この
懸濁物質は繊維ろ過器３２において除去される。繊維ろ
過器３２は、元々空隙率が高く、懸濁物質の保持容量が
大きい。そこで、沈殿処理水中の懸濁物質量が増えて
も、その繊維ろ過水における処理水質の変動はあまりな
い。沈殿処理水が、砂ろ過池３４に直接供給される場合
には、沈殿処理水中の懸濁物質量が増えるとすぐに目詰
まり発生などの問題が生じるが、繊維ろ過器３２を設け
ることでこのような問題が生じない。In such a water purification apparatus, the sedimentation basin 30
The suspended solids are removed in the fiber filter 32 even if fine flocs are contained in the settling water from the process. The fiber filter 32 originally has a high porosity and a large holding capacity for suspended substances. Therefore, even if the amount of suspended solids in the settling water increases, the quality of the treated water in the fiber filtration water does not vary much. When the sedimentation treatment water is directly supplied to the sand filtration pond 34, a problem such as clogging occurs as soon as the amount of suspended solids in the sedimentation treatment water increases. Such a problem does not occur.
【００２１】従って、本実施形態の浄水処理装置では、
沈殿池３０の表面負荷率を比較的大きくすることにより
沈殿池３０を小さくできる。また、繊維ろ過器３２は、
ろ過速度を大きくとれるため、小型にできる。そして、
本実施形態では、高分子混和池１８において、攪拌強度
を３００ｓ−１以上、滞留時間を５分以上に設定してい
る。これによって、高分子凝集剤が無機混和池１０から
供給される水と確実に混合される。そして、このような
比較的強力な攪拌によって、フロックサイズは小さくな
るが、高分子凝集剤に微細な懸濁物質が捕捉される。こ
のような凝集処理によって沈殿池３０で得られる上澄み
水は、比較的にＳＳの多いものとなる。しかし、これら
の多くは繊維ろ過器３２において除去される。そして、
砂ろ過池３４に供給される水には微細な懸濁質はほとん
ど含まれなくなり、砂ろ過池３４におけるろ過処理の負
荷を減少して好適なろ過処理が行える。Therefore, in the water treatment apparatus of the present embodiment,
By making the surface load rate of the sedimentation basin 30 relatively large, the size of the sedimentation basin 30 can be reduced. In addition, the fiber filter 32 is
Since the filtration speed can be increased, the size can be reduced. And
In the present embodiment, in the polymer mixing pond 18, the stirring intensity is set to 300 s -1 or more, and the residence time is set to 5 minutes or more. This ensures that the polymer flocculant is mixed with the water supplied from the inorganic mixing pond 10. Then, the floc size is reduced by such relatively intense stirring, but fine suspended substances are captured by the polymer flocculant. The supernatant water obtained in the sedimentation basin 30 by such coagulation treatment has a relatively large amount of SS. However, many of these are removed in the fiber filter 32. And
The water supplied to the sand filtration pond 34 hardly contains fine suspended solids, so that the load of the filtration treatment in the sand filtration pond 34 can be reduced and a suitable filtration treatment can be performed.
【００２２】すなわち、高分子凝集剤混合後の攪拌を弱
くすると、フロックは粗大化するが、微細な懸濁物質が
残り、砂ろ過池３４におけるろ過抵抗が大きくなる。本
実施形態によれば、攪拌強度の強い高分子混和池１８
と、繊維ろ過器３２と、砂ろ過池３４を組み合わせるこ
とによって、装置の全体としての大きさを小さくして、
良好な最終処理水を得ることができる。That is, when the stirring after mixing of the polymer flocculant is weakened, the floc is coarsened, but fine suspended substances remain, and the filtration resistance in the sand filtration pond 34 increases. According to the present embodiment, the polymer mixing pond 18 having a strong stirring intensity
By combining the fiber filter 32 and the sand filter 34, the overall size of the device is reduced,
Good final treated water can be obtained.
【００２３】なお、本実施形態では、無機凝集剤にＰＡ
Ｃを用いているが、硫酸バンド、塩化第二鉄、硫酸第二
鉄、ポリ硫酸アルミニウム・鉄等の鉄やアルミニウムを
原料とするものであれば、特に限定する必要はない。ま
た凝集助剤として、硫酸、塩酸、炭酸、水酸化ナトリウ
ム、消石灰等を加えることも好ましい。In the present embodiment, PA is used as the inorganic coagulant.
Although C is used, there is no particular limitation as long as iron or aluminum is used as a raw material such as a sulfate band, ferric chloride, ferric sulfate, and polyaluminum sulfate / iron. It is also preferable to add sulfuric acid, hydrochloric acid, carbonic acid, sodium hydroxide, slaked lime, or the like as a coagulation aid.
【００２４】本実施形態では、凝集池２６の前でのみ高
分子凝集剤の混和を行っているが、繊維ろ過器３２の前
でも高分子凝集剤の混和を行っても良い。また、繊維ろ
過器３２の前でのみ高分子凝集剤の混和を行っても良
い。In this embodiment, the mixing of the polymer flocculant is performed only before the flocculation pond 26, but the polymer flocculant may be mixed before the fiber filter 32. Further, the mixing of the polymer flocculant may be performed only before the fiber filter 32.
【００２５】[0025]
【実施例】（１）凝集沈殿ろ過法（比較例） 図１の構成から繊維ろ過器３２を省略した装置を用いて
実験を行った。この実験条件を以下に示す。EXAMPLES (1) Agglomerated sedimentation filtration method (comparative example) An experiment was conducted using an apparatus in which the fiber filter 32 was omitted from the configuration of FIG. The experimental conditions are shown below.
【００２６】「実験条件」 ・原水流量：１，０００ｍ３／時 ・無機混和池：滞留時間３分、撹拌強度２００ｓ−１ ・高分子混和池：滞留時間５分、撹拌強度６００ｓ−１ ・凝集池：横軸パドル３段式、滞留時間４０分 ・沈殿池：上向流式傾斜板付き沈殿池、滞留時間４０
分、上昇速度３ｍ／時 ・砂ろ過池：ケイ砂７００ｍｍ、有効径０．６ｍｍ、均
等係数１．３、ろ過速度１２０ｍ／日 ・原水濁度：３０度 ・原水ｐＨ：７．２ ・凝集剤：ＰＡＣ 注入率２０ｍｇ／ｌ ・凝集助剤：高分子凝集剤（ノニオン性アクリルアミド
ポリマー）、注入率０．３ｍｇ／Ｌ"Experimental conditions" Raw water flow rate: 1,000 m 3 / h Inorganic mixing pond: residence time 3 minutes, stirring intensity 200 s -1 Polymer mixing pond: residence time 5 minutes, stirring intensity 600 s -1 Coagulation Pond: Horizontal paddle three-stage type, residence time 40 minutes-Sedimentation basin: Upflow type sedimentation basin with inclined plate, residence time 40
Min, ascending speed 3m / h ・ Sand filtration tank: silica sand 700mm, effective diameter 0.6mm, uniformity coefficient 1.3, filtration speed 120m / day ・ Raw turbidity: 30 ° ・ Raw water pH: 7.2 ・ Coagulant : PAC injection rate 20 mg / l ・ Aggregation aid: high-molecular coagulant (nonionic acrylamide polymer), injection rate 0.3 mg / L
【００２７】このように、濁度３０度の原水に、凝集剤
としてＰＡＣ２０ｍｇ／Ｌを無機混和池１０で加え、急
速撹拌をＧ値２００ｓ−１で３分間行い、引き続き凝集
助剤として高分子凝集剤を高分子混和池１８で加え、急
速撹拌をＧ値６００ｓ−１で５分間行い、凝集池２６に
てフロック形成を行い、沈殿池３０にて沈殿分離を行っ
て、砂ろ過池３４にてろ過処理を行い処理水を得る。砂
ろ過池３４は４８時間に１回、空気逆流洗浄を通水速度
６０ｍ／時×５分間を行った後、逆流水洗浄を通水速度
３６ｍ／時×８分間行った。As described above, 20 mg / L of PAC as a coagulant was added to the raw water having a turbidity of 30 degrees in the inorganic mixing pond 10, and rapid stirring was performed at a G value of 200 s -1 for 3 minutes. The agent is added in the polymer mixing pond 18, rapid stirring is performed at a G value of 600 s −1 for 5 minutes, floc formation is performed in the coagulation pond 26, sedimentation and separation are performed in the sedimentation pond 30, and the sand filtration pond 34 is used. Filtration is performed to obtain treated water. The sand filtration basin 34 was subjected to air backflow cleaning at a flow rate of 60 m / hour × 5 minutes once every 48 hours, and then backflow water cleaning was performed at a water flow rate of 36 m / hour × 8 minutes.
【００２８】この時の各工程での濁度は、原水３０度、
沈殿処理水０．９度、ろ過水濁度０．０４度となってい
た。また砂ろ過池の通水時間４８時間でのろ過抵抗は、
１，５００ｍｍであった。At this time, the turbidity in each step was 30 degrees in raw water,
The precipitation-treated water was 0.9 ° and the turbidity of the filtered water was 0.04 °. In addition, the filtration resistance of the sand filtration pond during 48 hours of water flow is as follows:
1,500 mm.
【００２９】（２）凝集沈殿ろ過法（実施形態） 図１の装置を用いて実験を行った。実験条件を以下に示
す。(2) Coagulation-sedimentation filtration method (Embodiment) An experiment was conducted using the apparatus shown in FIG. The experimental conditions are shown below.
【００３０】［実験条件］ ・原水流量：１，０００ｍ３／時 ・無機混和池：滞留時間３分、撹拌強度 ２００ｓ−１ ・高分子混和池：滞留時間５分、撹拌強度 ６００ｓ
−１ ・凝集池：横軸パドル３段式、滞留時間４０分 ・沈殿池：上向流式傾斜板付き沈殿池、滞留時間２０
分、上昇速度６ｍ／時 ・繊維ろ過器：アクリル製長繊維ろ材、ろ材長１５０ｃ
ｍ、充填密度１００ｋｇ／ｍ２、ろ過速度 ４８０ｍ／
日（２０ｍ／時） ・砂ろ過池：ケイ砂７００ｍｍ、有効径０．６ｍｍ、均
等係数 １．３、ろ過速度２４０ｍ／日 ・原水濁度：３０度 ・原水ｐＨ：７．２ ・凝集剤：ＰＡＣ 注入率２０ｍｇ／ｌ ・凝集助剤：高分子凝集剤（ノニオン性アクリルアミド
ポリマー）、注入率０．３ｍｇ／Ｌ[Experimental conditions]-Raw water flow rate: 1,000 m 3 / hour-Inorganic mixing pond: residence time 3 minutes, stirring intensity 200 s- 1 -Polymer mixing pond: residence time 5 minutes, stirring intensity 600 s
-1. Coagulation pond: 3-stage horizontal paddle type, residence time 40 minutes.-Sedimentation basin: upward flow type sedimentation basin with inclined plate, residence time 20.
Min, ascending speed 6m / h ・ Fiber filter: acrylic long fiber filter media, filter media length 150c
m, packing density 100 kg / m 2 , filtration speed 480 m / m
Day (20 m / hr)-Sand filter: sand sand 700 mm, effective diameter 0.6 mm, uniformity coefficient 1.3, filtration speed 240 m / day-Raw water turbidity: 30 degrees-Raw water pH: 7.2-Flocculant: PAC Injection rate 20 mg / l Coagulation aid: High-molecular coagulant (nonionic acrylamide polymer), injection rate 0.3 mg / L
【００３１】濁度３０度の原水に、凝集剤としてＰＡＣ
２０ｍｇ／Ｌを無機混和池１０で加え、急速撹拌をＧ値
２００ｓ−１で３分間行い、引き続き凝集助剤として高
分子凝集剤を高分子混和池１８で加え、急速撹拌をＧ値
６００ｓ−１で５分行い、凝集池２６にてフロック形成
を行い、沈殿池３０にて固液分離を行って、さらに繊維
ろ過器３２にて粗ろ過を行った後、砂ろ過池３４にてろ
過処理を行い処理水を得る。繊維ろ過器３２は２４時間
に１回、水・空気逆流洗浄を水通水速度１００ｍ／時、
空気通水速度３００ｍ／時で６分間行っている。砂ろ過
池３４は４８時間に１回、空気逆流洗浄を通水速度６０
ｍ／時×５分間行った後、逆流水洗浄を通水速度３６ｍ
／時×８分間行った。In raw water having a turbidity of 30 degrees, PAC is used as a flocculant.
20 mg / L was added in the inorganic mixing pond 10 and rapid stirring was performed at a G value of 200 s -1 for 3 minutes. Subsequently, a polymer flocculant was added as a coagulant in the polymer mixing pond 18 and the rapid stirring was performed with a G value of 600 s -1. After 5 minutes, floc formation is performed in the flocculation pond 26, solid-liquid separation is performed in the sedimentation pond 30, coarse filtration is performed in the fiber filter 32, and then filtration is performed in the sand filter 34. To obtain treated water. The fiber filter 32 performs water / air backwashing once every 24 hours with a water flow rate of 100 m / hour.
The air flow rate is 300 m / h for 6 minutes. The sand filtration pond 34 has a backflow air cleaning rate of 60 once every 48 hours.
m / hour x 5 minutes, then backflow water washing 36m
/ Hour × 8 minutes.
【００３２】この時の各工程での濁度は、原水３０度、
沈殿処理水１．２度（比較例０．９度）、繊維ろ過処理
水濁度０．１度、砂ろ過水濁度０．０３度（比較例０．
０４度）となっていた。沈殿処理水濁度で比べると、比
較例よりも高い値となっているが、繊維ろ過処理水つま
り砂ろ過供給水では、比較例よりも低い値となってい
る。また砂ろ過池の通水時間４８時間でのろ過抵抗は、
ろ過速度が従来法の２倍であるにも拘わらず７００ｍｍ
と比較例のろ過抵抗１，５００ｍｍの半分以下であっ
た。At this time, the turbidity in each step was 30 degrees in raw water,
Precipitation treatment water 1.2 degrees (Comparative Example 0.9 degrees), fiber filtration treatment water turbidity 0.1 degrees, sand filtration water turbidity 0.03 degrees (Comparative Example 0.
04 degrees). When compared with the turbidity of the sedimentation treatment water, the value is higher than that of the comparative example, but the value of the fiber filtration treatment water, that is, the supply water of sand filtration is lower than that of the comparative example. In addition, the filtration resistance of the sand filtration pond during 48 hours of water flow is as follows:
700mm despite the double filtration speed of the conventional method
And the filtration resistance of the comparative example was not more than half of 1,500 mm.
【００３３】比較例の各設備の設置面積を１００とした
場合の設置面積を比較すると、表１の様に沈殿池で５０
％、ろ過池（本発明では繊維ろ過器＋砂ろ過池）で７５
％に縮小できている。Comparing the installation area with the installation area of each facility of the comparative example assuming that the installation area is 100, as shown in Table 1, 50
%, 75 in the filter pond (fiber filter + sand filter in the present invention)
%.
【表１】 [Table 1]
【００３４】[0034]
【発明の効果】以上説明したように、本発明によれば、
比較的強い攪拌で、有機高分子凝集剤を混合すること
で、有機高分子凝集剤により、微細な懸濁物質を捕捉す
ることができる。一方、このような強い攪拌を行うと、
フロック径が十分大きくならず、微細フロックが沈殿池
より流出する可能性が高いが、これは繊維ろ過で除去す
ることができる。繊維ろ過器はろ過速度を大きくとれる
ため、装置の全体としての大きさ（浄水装置全体）を小
さくできる。そして、繊維ろ過器の処理水には、微細懸
濁物質が非常に少ないため、砂ろ過供給水濁度が安定
し、砂ろ過装置におけるろ過抵抗の低減が図れる。As described above, according to the present invention,
By mixing the organic polymer flocculant with relatively strong stirring, fine suspended substances can be captured by the organic polymer flocculant. On the other hand, when such strong stirring is performed,
The floc diameter is not large enough, and there is a high possibility that the fine floc flows out of the sedimentation basin, which can be removed by fiber filtration. Since the filtration speed of the fiber filter can be increased, the overall size of the apparatus (the entire water purification apparatus) can be reduced. And, since there is very little fine suspended substance in the treated water of the fiber filter, the turbidity of the sand filtration supply water is stabilized, and the filtration resistance in the sand filtration device can be reduced.
【図１】 実施形態の装置の全体構成を示す図である。FIG. 1 is a diagram illustrating an overall configuration of an apparatus according to an embodiment.
１０ 無機混和池、１８ 高分子混和池、２０ 攪拌装
置、２６ 凝集池、３０ 沈殿池、３２ 繊維ろ過器、
３４ 砂ろ過池。10 inorganic mixing pond, 18 polymer mixing pond, 20 stirrer, 26 coagulation pond, 30 sedimentation pond, 32 fiber filter,
34 Sand filtration pond.
───────────────────────────────────────────────────── フロントページの続き (51)Int.Cl.7 識別記号 ＦＩ テーマコート゛(参考） Ｂ０１Ｄ 23/16 Ｆターム(参考） 4D015 BA12 BA19 BB08 BB12 CA14 DA04 DA05 DA06 DA13 DA16 DB03 DC07 DC08 EA06 FA15 FA16 4D041 BA01 BB04 BB10 CA04 CB03──────────────────────────────────────────────────続 き Continued on the front page (51) Int.Cl. 7 Identification symbol FI Theme coat ゛ (Reference) B01D 23/16 F term (Reference) 4D015 BA12 BA19 BB08 BB12 CA14 DA04 DA05 DA06 DA13 DA16 DB03 DC07 DC08 EA06 FA15 FA16 4D041 BA01 BB04 BB10 CA04 CB03
Claims (3)
を混合し凝集沈殿処理を行う凝集沈殿処理装置と、凝集
沈殿処理水について砂ろ過処理を行う砂ろ過装置を有す
る浄水処理装置であって、 前記有機高分子凝集剤の混和を撹拌強度Ｇ値で３００〜
１０００ｓｅｃ−１で５分以上行うとともに、 前記砂ろ過装置の前段で繊維をろ材に用いた繊維ろ過装
置による粗ろ過処理を行うことを特徴とする浄水処理装
置。The present invention relates to a water purification treatment apparatus having a coagulation / sedimentation treatment apparatus for mixing and coagulating sedimentation treatment with an organic polymer coagulant after mixing an inorganic coagulant, and a sand filtration apparatus for performing sand filtration treatment on coagulation / sedimentation treatment water. The mixing of the organic polymer flocculant is 300 to
A water purification treatment device, wherein the treatment is performed at 1000 sec -1 for 5 minutes or more, and a coarse filtration treatment is performed by a fiber filtration device using fibers as a filter material in a preceding stage of the sand filtration device.
記繊維ろ過装置のろ過速度が１０ｍ／時以上であること
を特徴とする浄水処理装置。2. The water purifying apparatus according to claim 1, wherein the surface load factor of the coagulating sedimentation device is 3.5 m / h or more, and the filtration speed of the fiber filtration device is 10 m / h or more. Processing equipment.
て、 前記繊維ろ過装置のろ材が長さ５０ｃｍ〜３００ｃｍの
長繊維束であることを特徴とする浄水処理装置。3. The apparatus according to claim 1, wherein the filter medium of the fiber filtration device is a long fiber bundle having a length of 50 cm to 300 cm.
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Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002292207A (en) * | 2001-03-30 | 2002-10-08 | Japan Organo Co Ltd | Apparatus for treating water |
| JP2006043626A (en) * | 2004-08-06 | 2006-02-16 | Hara Giken Kogyo:Kk | Water treatment apparatus |
| JP2017159199A (en) * | 2016-03-07 | 2017-09-14 | 株式会社東芝 | Solid-liquid separator and control device |
| JP2018192453A (en) * | 2017-05-22 | 2018-12-06 | オルガノ株式会社 | Membrane filtration apparatus and method |
-
2001
- 2001-03-08 JP JP2001064293A patent/JP3854471B2/en not_active Expired - Fee Related
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2002292207A (en) * | 2001-03-30 | 2002-10-08 | Japan Organo Co Ltd | Apparatus for treating water |
| JP4523731B2 (en) * | 2001-03-30 | 2010-08-11 | オルガノ株式会社 | Water treatment equipment |
| JP2006043626A (en) * | 2004-08-06 | 2006-02-16 | Hara Giken Kogyo:Kk | Water treatment apparatus |
| JP2017159199A (en) * | 2016-03-07 | 2017-09-14 | 株式会社東芝 | Solid-liquid separator and control device |
| JP2018192453A (en) * | 2017-05-22 | 2018-12-06 | オルガノ株式会社 | Membrane filtration apparatus and method |
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