JPS6143083B2 - - Google Patents
Info
- Publication number
- JPS6143083B2 JPS6143083B2 JP54030183A JP3018379A JPS6143083B2 JP S6143083 B2 JPS6143083 B2 JP S6143083B2 JP 54030183 A JP54030183 A JP 54030183A JP 3018379 A JP3018379 A JP 3018379A JP S6143083 B2 JPS6143083 B2 JP S6143083B2
- Authority
- JP
- Japan
- Prior art keywords
- water
- polluted wastewater
- filtration
- polluted
- raw water
- 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
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 58
- 238000001914 filtration Methods 0.000 claims description 36
- 239000002351 wastewater Substances 0.000 claims description 32
- 239000000463 material Substances 0.000 claims description 28
- 239000008187 granular material Substances 0.000 claims description 3
- 238000007599 discharging Methods 0.000 claims description 2
- 238000000034 method Methods 0.000 description 9
- 238000000926 separation method Methods 0.000 description 7
- VYPSYNLAJGMNEJ-UHFFFAOYSA-N Silicium dioxide Chemical compound O=[Si]=O VYPSYNLAJGMNEJ-UHFFFAOYSA-N 0.000 description 6
- 238000004140 cleaning Methods 0.000 description 5
- 230000008929 regeneration Effects 0.000 description 4
- 238000011069 regeneration method Methods 0.000 description 4
- 238000004064 recycling Methods 0.000 description 3
- 230000001172 regenerating effect Effects 0.000 description 3
- 238000010586 diagram Methods 0.000 description 2
- 239000000706 filtrate Substances 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000000377 silicon dioxide Substances 0.000 description 2
- 239000010802 sludge Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 206010016803 Fluid overload Diseases 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 238000005345 coagulation Methods 0.000 description 1
- 230000015271 coagulation Effects 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 239000002223 garnet Substances 0.000 description 1
- 230000005484 gravity Effects 0.000 description 1
- 239000007788 liquid Substances 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000005406 washing Methods 0.000 description 1
Landscapes
- Filtration Of Liquid (AREA)
Description
本発明は移動床過装置を用いた過方法に関
するものである。
移動床式過方法は硅砂、アンスラサイト、ガ
ーネツトなどの細かい粒状材（単に材と略
す）を筒内に充填し、その過層の一部を順次取
出し、洗浄再生を行い、再度補給する、いわゆる
循環再生を行いつつ、被過水（以下原水と略
す）を過筒へ通水し過目的を達する方法であ
る。過筒内原水の流れは下向流、上向流、放射
流などの方法が取られ、また材の移動は過筒
底部から抜取り、上部へ返す下向移動が多く。そ
の移動方法にエアーリフト式、ウオータージエツ
ト式、スクリユーコンベアー式等が多く取られ
る。
この方法による移動床式過法は従来使われて
いる層が固定状態にある固定過法に比較して
連続で層を洗浄再生しつつ、過を達成するた
めに、流量低下がなく、原水通水を停止しての洗
浄操作が不要であり、更に原水濃度が大きく変動
しても、層の閉塞という現象がないなどの長所
を有している。しかし反面、次のような欠点を持
つている。連続洗浄を行うがために洗浄により生
じた汚濁排水が連続的に排出され、その量は従来
の固定過法が処理量Ｑm3/d当り、２〜４％で
あるのに対し、８〜16％と比較的多く排出され
る。汚濁排水量が多ければ付属設備としての処理
規模が大きくなる。あるいは既存の活性汚泥処理
設備、凝集沈殿処理設備等の後処理に適用した場
合、これら処理設備に返送水としての汚濁排水が
多量に返送されると沈殿池の固液分離に支障をき
たし、浮遊懸濁物質（SSと略す）のキヤリーオ
ーバーとなる。これがまた過装置の原水とな
り、SSが更に高くなることから、過水の水質
も悪るくなるなどの悪循環を起すことになる。
本発明はかかる観点から移動床式過装置を用
いた場合に発生する汚濁排水量を極力抑え、他系
統での処理負担を軽減する移動床式過方法を提
供するものである。
本発明は原水を過する主過装置で過処理
水を得、主過装置から発生する汚濁排水を原水
として過を行う補助過装置を設け、この補助
過装置で汚濁排水を再濃縮し、該過系から発
生する汚濁排水を著しく低減する方法である。
すなわち、本発明は粒状材を充填した過筒
底部より材を抜き取り、該材を再生し過筒
上部へ補給しつつ、被処理水を通水するようにな
した移動床過装置を２装置以上連結し、前位の
装置で得られた汚濁排水を次位の装置の被過水
とし、次位の装置の過水を前位の装置の被過
水に混入させ、最終位の汚濁排水のみを系外に排
出させることを特徴とする移動床式過方法に関
し、過系から発生する汚濁排水量を少くするこ
とができる方法である。
本発明を更に以下実施例により説明する。
図面は本発明の過方法を示す説明図で、原水
の流れは過筒の底部から入り、上部から過水
として出す上向流過方法である。図では明示し
ていないが、原水の流れを下向流とする過方式
でも以下の説明において原水の流れを下向にする
ことで適用できる。この図では装置を２つ連結
し、前位のものを主過装置、次位のものを補助
過装置とする。
被過水１は材２を充填した主過装置３の
底部にある導入口４から導入する。導入された原
水１は材２層を上昇する間に含有するSSが除
かれ、過処理水５として出る。SSを捕捉した
材２層は順次連続的に下降し、主過装置３の
下部にある材移送口６に達し、ここからエア−
７の供給を受け、エアーリフトによりリフトパイ
プ８を上昇する。この場合、エアーリフトの他に
ウオータージエツト、あるいはスクリユーコンベ
アなどのリフト方法を用いてもよい。
材２に捕捉されたSSはリフトパイプ８中で
剥離され材空隙に含む自由水側に移る。リフト
された材２は材再生分離筒９に達し、ここで
材２とSSを多量に含んだ汚濁排水１０ａとに
分別される。材２は汚濁排水１０ａに比較して
比重が著しく大きい（硅砂の場合2.65）ために
SSよりも先に沈降し、材再生分離筒９ａと９
ｂの間を下り、主過装置３の材２層の上部へ
供給される。即ち材２はSS捕捉と洗浄である
再生を連続的に受け、主過装置３を循環する。
材再生分離筒９を下る材２に含む自由水は
浄化された水と置換されるように過処理水５の
出口水位が汚濁排水１０ａの出口水位より高い位
置とし、材２層を通る過水１１の少量が材
再生分離筒９ａ−９ｂ間を上昇するようにしてあ
る。従つて汚濁排水１０ａはリフトされてくる
材２間の自由水と同量、もしくはそれ以上となつ
て排出される。ここで過処理水５の水質をよく
する、即ちSSを高度に除去する場合、リフトさ
れてくる材２間の自由水をほぼ完全に過水１
１で追い出し、材再生分離筒９ａ−９ｂ間を下
る材２間の自由水が過水１１で置換されなけ
ればならない。このために汚濁排水１０ａは原水
１のＱm3/d当り８〜16％の多い量となる。従つ
て汚濁排水１０ａを減少させるために、これを更
に補助過装置１２へ導入する。
導入方法はポンプ圧送でもよく、また落差が十
分にある場合は水位差で導入可能である。
補助過装置１２の機構は全く主過装置２と
同様である。汚濁排水１０ａは補助過水１３と
汚濁排水１０ｂとに分別される。補助過水１３
は主過装置２の原水１に混入させる。この場
合、補助過水１３のSSはほぼ原水１と同程度
のSS濃度となり、また多少高くても原水１で10
倍程度に稀釈されることから、原水に混入させて
も向等問題とならない。従つて過処理水５は高
度に過されたものとなる。また汚濁排水１０ａ
は補助過装置１２で約1/10に減少する。
逆にSS濃度からみると約10倍に濃縮された汚
濁排水１０ｂとなる。従つて全過系から発生す
る汚濁排水量はＱm3/d（被過水１）×0.1（汚濁
排水１０ａ）×0.1（汚濁排水１０ｂ）＝0.01Qm3/d
となり約１％に減少する。
主装置、補助装置の２つで所望の減少が得られ
なければさらに次の補助装置を連結する。
ここで活性汚泥処理水、いわゆる二次処理水を
図面に示す装置を使つて過運転を行つた。その
結果を表１に示す。汚濁排水は1.3％、過処理
水SSは４mg/が得られ、十分に効果を発揮して
いる。
移動床過装置による過方法では、それから
発生する汚濁排水が原水量の10％程度多く発生し
ていた。
本発明による主過装置からの汚濁排水を補助
過装置に通し、該過水を主過装置の原水に
混入させることにより全過系から発生する汚濁
排水量を著しく低減することが可能となり、その
発生量を１％程度とすることができた。
これにより、汚濁排水の別系処理が著しく容易
となり経済的負担も著しく軽減される。
The present invention relates to a filtration method using a moving bed filtration device. The moving bed filtration method involves filling a cylinder with fine granular material (abbreviated simply as material) such as silica sand, anthracite, and garnet, and sequentially taking out part of the excess layer, washing and regenerating it, and replenishing it again. This is a method to achieve the purpose of overflow by passing overwater (hereinafter referred to as raw water) to the overtube while performing cyclical regeneration. Methods such as downward flow, upward flow, and radial flow are used for the flow of raw water in the tube, and materials are often moved downward by being extracted from the bottom of the tube and returned to the top. Air lift type, water jet type, screw conveyor type, etc. are often used as the transportation method. Compared to the conventional fixed filtration method in which the bed is in a fixed state, this moving bed filtration method achieves filtration while continuously cleaning and regenerating the bed, so there is no flow rate drop and the raw water can pass through. It has the advantage that there is no need to perform a cleaning operation by stopping the water supply, and there is no phenomenon of layer blockage even if the raw water concentration fluctuates greatly. However, on the other hand, it has the following drawbacks. Due to continuous cleaning, polluted wastewater generated by cleaning is continuously discharged, and the amount is 8 to 16% per treatment amount Qm 3 /d, compared to 2 to 4% in the conventional fixed filtration method. %, a relatively large amount is emitted. The larger the amount of polluted wastewater, the larger the scale of treatment as ancillary equipment. Alternatively, when applied to the after-treatment of existing activated sludge treatment equipment, coagulation sedimentation treatment equipment, etc., if a large amount of polluted wastewater is returned to these treatment equipment as return water, it will interfere with solid-liquid separation in the sedimentation tank, resulting in suspended solids. This is a carryover of suspended solids (abbreviated as SS). This also becomes raw water for the filtration equipment, which further increases the SS, causing a vicious cycle in which the quality of the filtrated water deteriorates. From this point of view, the present invention provides a moving bed filtration method that minimizes the amount of polluted wastewater generated when a moving bed filtration device is used and reduces the processing burden on other systems. The present invention obtains over-treated water using a main filtration device that filters raw water, provides an auxiliary filtration device that filters contaminated wastewater generated from the main filtration device as raw water, and reconcentrates the polluted wastewater with this auxiliary filtration device. This method significantly reduces the amount of polluted wastewater generated from the wastewater system. That is, the present invention provides two or more moving bed filtration devices that extract material from the bottom of the overtube filled with granular material, regenerate the material, and replenish it to the top of the overtube while passing water to be treated. The polluted wastewater obtained from the previous device is used as overflow water for the next device, the excess water from the next device is mixed with the overflow water from the previous device, and only the polluted wastewater from the last device is connected. Regarding a moving bed type filtration method characterized by discharging wastewater out of the system, this method can reduce the amount of polluted wastewater generated from the filtration system. The present invention will be further explained below with reference to Examples. The drawing is an explanatory diagram showing the filtration method of the present invention, which is an upward flow filtration method in which the flow of raw water enters from the bottom of the sieve tube and is discharged from the top as filtrate. Although not clearly shown in the figure, a flow method in which the flow of raw water is made downward can also be applied by making the flow of raw water downward in the following explanation. In this figure, two devices are connected, with the front one being the main passing device and the next one being the auxiliary passing device. The overflow water 1 is introduced from the inlet 4 at the bottom of the main filtration device 3 filled with material 2. While the introduced raw water 1 rises through the 2nd layer of material, the SS contained therein is removed and comes out as supertreated water 5. The two layers of material that have captured SS descend one after another and reach the material transfer port 6 at the bottom of the main filtration device 3, from which air is drawn.
7 is supplied, and the lift pipe 8 is raised by an air lift. In this case, a lifting method such as a water jet or a screw conveyor may be used in addition to an air lift. The SS trapped in the material 2 is separated in the lift pipe 8 and transferred to the free water side contained in the material voids. The lifted material 2 reaches the material recycling separation tube 9, where it is separated into the material 2 and polluted waste water 10a containing a large amount of SS. Material 2 has a significantly higher specific gravity (2.65 in the case of silica sand) compared to polluted wastewater 10a.
It settles before the SS, and the material regenerating separation cylinders 9a and 9
b, and is supplied to the upper part of the two layers of material of the main filtration device 3. That is, the material 2 is continuously subjected to regeneration, which is SS capture and cleaning, and is circulated through the main filtration device 3. The outlet water level of the supertreated water 5 is set higher than the outlet water level of the polluted waste water 10a so that the free water contained in the material 2 flowing down the material recycling separation tube 9 is replaced with purified water. A small amount of 11 is made to rise between the material regeneration separation cylinders 9a and 9b. Therefore, the polluted waste water 10a is discharged in an amount equal to or more than the free water between the lifted materials 2. In order to improve the water quality of the over-treated water 5, that is, to remove SS to a high degree, the free water between the lifted materials 2 is almost completely replaced by the over-treated water 1.
1, the free water between the materials 2 that flows down between the material regeneration separation cylinders 9a and 9b must be replaced with superhydrous water 11. For this reason, the amount of polluted wastewater 10a becomes 8 to 16% per Qm 3 /d of raw water 1. Therefore, in order to reduce the polluted waste water 10a, it is further introduced into the auxiliary filtration device 12. The introduction method may be by pump force feeding, or if there is a sufficient head difference, introduction can be made by using a water level difference. The mechanism of the auxiliary filtration device 12 is completely similar to that of the main filtration device 2. The polluted wastewater 10a is separated into an auxiliary superfluous water 13 and a polluted wastewater 10b. Auxiliary overhydration 13
is mixed into the raw water 1 of the main filtration device 2. In this case, the SS concentration of auxiliary superhydrous water 13 is almost the same as that of raw water 1, and even if it is slightly higher, it is 10% in raw water 1.
Since it can be diluted to about twice as much, mixing it with raw water does not pose a problem. Therefore, the overtreated water 5 becomes highly filtered. Also, polluted wastewater 10a
is reduced to about 1/10 by the auxiliary filter 12. Conversely, in terms of SS concentration, the polluted wastewater 10b is about 10 times more concentrated. Therefore, the amount of polluted wastewater generated from the total flow system is Qm 3 /d (overflow water 1) x 0.1 (polluted wastewater 10a) x 0.1 (polluted wastewater 10b) = 0.01Qm 3 /d
This decreases to approximately 1%. If the desired reduction is not achieved with both the main device and the auxiliary device, the next auxiliary device is connected. Here, activated sludge treated water, so-called secondary treated water, was over-operated using the equipment shown in the drawing. The results are shown in Table 1. Contaminated wastewater was obtained at 1.3%, and over-treated water SS was obtained at 4 mg/ml, indicating that it is sufficiently effective. In the filtration method using a moving bed filtration device, approximately 10% more contaminated wastewater was generated than the amount of raw water. By passing the polluted wastewater from the main filtration device according to the present invention to the auxiliary filtration device and mixing the filtrate into the raw water of the main filtration device, it is possible to significantly reduce the amount of polluted wastewater generated from the total filtration system, and its occurrence. The amount could be reduced to about 1%. This greatly facilitates the separate treatment of polluted wastewater and significantly reduces the economic burden.
【表】【table】
図面は本発明の一実施例を示す過方法の説明
図である。
符号の説明、１……被過水（原水）、２……
材、３……主過装置、４……導入口、５……
過処理水、６……材移送口、７……エアー、
８……リフトパイプ、９……材再生分離筒、０
……汚濁排水、１１……過水、１２……補助
過装置、１３……補助過水。
The drawings are explanatory diagrams of a method showing an embodiment of the present invention. Explanation of symbols, 1... Overflow water (raw water), 2...
Material, 3... Main passage device, 4... Inlet, 5...
Overtreated water, 6... Material transfer port, 7... Air,
8...Lift pipe, 9...Material recycling separation cylinder, 0
...Dirty drainage, 11...Overwatering, 12...Auxiliary filtration device, 13...Auxiliary overwatering.
Claims (1)
き取り、該材を再生し過筒上部へ補給しつ
つ、被過水を通水するようになした移動床過
装置を２装置以上連結し、前位の装置で得られた
汚濁排水を次位の装置の被過水とし、次位の装
置の過水を前位の装置の被過水に混入させ、
最終位の汚濁排水のみを系外に排出させることを
特徴とする移動床式過方法。1 Two or more moving bed filtration devices are connected to each other in such a way that the material is extracted from the bottom of the tube filled with granular material, recycled, and replenished to the top of the tube, while passing water through the tube. The polluted wastewater obtained from the next equipment is used as overflow water for the next equipment, and the excess water from the next equipment is mixed into the overflow water from the previous equipment.
A moving bed filtration method characterized by discharging only the last polluted wastewater out of the system.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3018379A JPS55121814A (en) | 1979-03-14 | 1979-03-14 | Moving bed type filtrating method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP3018379A JPS55121814A (en) | 1979-03-14 | 1979-03-14 | Moving bed type filtrating method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS55121814A JPS55121814A (en) | 1980-09-19 |
| JPS6143083B2 true JPS6143083B2 (en) | 1986-09-25 |
Family
ID=12296639
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP3018379A Granted JPS55121814A (en) | 1979-03-14 | 1979-03-14 | Moving bed type filtrating method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS55121814A (en) |
Families Citing this family (2)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6426005B1 (en) * | 2000-04-18 | 2002-07-30 | Parkson Corporation | Sequential descending bed filters with reject/washwater containing impurities being fed to a separate unit for elimination of impurities |
| ES2267360B1 (en) * | 2004-12-15 | 2008-03-01 | Yarob Tilouni Yosef | "WATER FILTRATION EQUIPMENT BY SAND IN DOUBLE STAGE WITH CONTINUOUS SAND WASHING". |
-
1979
- 1979-03-14 JP JP3018379A patent/JPS55121814A/en active Granted
Also Published As
| Publication number | Publication date |
|---|---|
| JPS55121814A (en) | 1980-09-19 |
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