JPS597485B2 - Upflow moving bed filtration device - Google Patents
Upflow moving bed filtration deviceInfo
- Publication number
- JPS597485B2 JPS597485B2 JP52122170A JP12217077A JPS597485B2 JP S597485 B2 JPS597485 B2 JP S597485B2 JP 52122170 A JP52122170 A JP 52122170A JP 12217077 A JP12217077 A JP 12217077A JP S597485 B2 JPS597485 B2 JP S597485B2
- Authority
- JP
- Japan
- Prior art keywords
- liquid
- tank
- separation tank
- filter medium
- 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.)
- Expired
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- Filtration Of Liquid (AREA)
Description
【発明の詳細な説明】
本発明は上向流移動層式濾過装置に関し、詳しくは濾過
槽に再生濾材を搬送液と共に供給しても、搬送液の混入
による処理液の品質の低下を招くことなく、高品質の処
理液を得ることができる上向流移動層式濾過装置に関す
る。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to an upflow moving bed type filtration device, and more particularly, even if a regenerated filter medium is supplied to a filtration tank together with a carrier liquid, the quality of the treated liquid may deteriorate due to contamination with the carrier liquid. The present invention relates to an upflow moving bed type filtration device that can obtain a high-quality processing liquid.
上向流移動層式濾過装置においては、懸濁物質（以下、
ＳＳという。In an upflow moving bed type filtration device, suspended solids (hereinafter referred to as
It's called SS.
）を捕捉した濾材は、通常、濾過槽下端から抜出され、
洗滌再生後、再使用に供するため、濾過槽上部に搬送さ
れる。) is usually extracted from the bottom of the filtration tank,
After washing and regeneration, it is transported to the upper part of the filtration tank for reuse.
従来、再生濾材を濾過槽に搬送するには、普通、濾過槽
で濾過処理された処理液の一部を用い、エゼクター等に
より固液混相流とする場合が多いが、このようにすれば
、濾材の再生が十分に行なわれていたとしても、尚、濾
材には幾分のＳＳが付着していることは免れず、従って
、再生濾材が固液混相流で濾過槽に搬送される過程で、
濾材に付着していたＳＳが離脱し、搬送液中に移行する
から、この搬送液が濾過槽内で処理液と混じって、処理
液の品質を悪化させる欠点があった。Conventionally, in order to convey the regenerated filter medium to the filtration tank, a part of the treated liquid that has been filtered in the filtration tank is often used and converted into a solid-liquid multiphase flow using an ejector or the like. Even if the filter media has been sufficiently regenerated, it is inevitable that some SS will adhere to the filter media, and therefore, during the process of the regenerated filter media being conveyed to the filtration tank in a solid-liquid multiphase flow. ,
Since the SS adhering to the filter medium is detached and transferred into the carrier liquid, this carrier liquid mixes with the processing liquid in the filtration tank, resulting in a disadvantage that the quality of the processing liquid deteriorates.
特に、この欠点は処理液に高度の品質が要求される場合
に致命的である。In particular, this drawback is fatal when a high level of quality is required of the processing liquid.
本発明は上記問題点を解決するためになされたものであ
って、濱過槽に再生濾材を搬送液と共に供給した際、搬
送液と処理液とが実質的に混じり合わず、従って、処理
液の品質を高度に維持し得る上向流移動層式濾過装置を
提供することを目的とする。The present invention has been made to solve the above-mentioned problems, and when the regenerated filter medium is supplied to the filtering tank together with the carrier liquid, the carrier liquid and the treatment liquid do not substantially mix. An object of the present invention is to provide an upflow moving bed type filtration device that can maintain a high level of quality.
本発明は粒子状濾材を下方に移動させつつ、瀘過槽下部
より被処理液を導入して濾過槽上部より処理液として取
出すようにした上向流移動層式濾過装置において、濾過
槽１の上に搬送されてきた再生濾材とその搬送液とを分
離する分離槽３を併設すると共に、その分離槽下端部３
ａに連続して形成した再生濾材排出用及び抵抗部材とし
ての挿入管６を前記濾過槽１内の濾材層上面２０ａまで
挿入して分離槽３内の再生濾材２を挿入管６を介して濾
過槽１内の濾材層に連続させ、前記分離槽３の略中段部
に再生濾材を搬送液と共に分離槽３に供給する再生濾材
供給口４を、分離槽３の上部に前記搬送液を分離槽３か
ら流出させる搬送液出口５をそれぞれ設け、一方、上記
濾過槽１の上部から処理液を外部に取出す処理液管１０
を濾過槽１より上方で前記搬送液出口５よりもｈｔ（ｈ
ｘ＞０）だけ低い位置で大気圧下に開口１０ａすること
により、該処理液管１０の開口位置における位置水頭と
管１０内での圧損水頭との和が前記分離槽下端部６より
も高く且つ搬送液出口５よりもｈ２（ｈｚ＞Ｏ）だけ低
いレベルＬに相当する位置水頭になるようにすると共に
、該ｈ２に相当する位置水頭が前記レベルＬから挿入管
６下端までの圧損水頭と処理液管１０の圧損水頭との和
よりも低くなるようにしたことを特徴とする。The present invention provides an upward flow moving bed filtration device in which a liquid to be treated is introduced from the lower part of the filtration tank and taken out as a treated liquid from the upper part of the filtration tank while moving the particulate filter medium downward. A separation tank 3 is installed to separate the regenerated filter medium transported above from its transport liquid, and a lower end portion 3 of the separation tank is installed.
An insertion tube 6 for discharging recycled filter media and as a resistance member, which is formed continuously in a, is inserted into the filter tank 1 up to the upper surface 20a of the filter media layer, and the recycled filter media 2 in the separation tank 3 is filtered through the insertion tube 6. A regenerated filter medium supply port 4 is connected to the filter medium layer in the tank 1 and is connected to a substantially middle part of the separation tank 3 for supplying the regenerated filter medium to the separation tank 3 together with the conveying liquid. 3, and a processing liquid pipe 10 for taking out the processing liquid to the outside from the upper part of the filtration tank 1.
ht (h
x>0), the sum of the positional head at the opening position of the processing liquid pipe 10 and the pressure drop head within the pipe 10 is higher than that at the lower end 6 of the separation tank. In addition, the position head corresponding to level L is set to be h2 (hz>O) lower than the conveyed liquid outlet 5, and the position head corresponding to h2 is equal to the pressure loss head from the level L to the lower end of the insertion tube 6. It is characterized in that it is lower than the sum of the pressure loss head of the processing liquid pipe 10.
以下実施例を示す図面に基づいて本発明を詳細に説明す
る。The present invention will be described in detail below based on drawings showing embodiments.
第１図、第２図に示す装置において、濾過槽１の上端に
、再生濾材２と搬送液とを分離するための分離槽３が併
設され、分離槽３の略中段部には再生濾材を搬送液と共
に固液混相流にて分離槽３に供給する再生瀘材供給口４
が、また、分離槽３の上部には搬送液を流出させる搬送
液出口５がそれぞれ設けられている。In the apparatus shown in FIGS. 1 and 2, a separation tank 3 for separating a regenerated filter medium 2 and a conveyed liquid is provided at the upper end of a filtration tank 1, and a regenerated filter medium is installed approximately in the middle of the separation tank 3. Recycled filter material supply port 4 that supplies a solid-liquid multiphase flow to the separation tank 3 together with the conveyed liquid
However, the upper part of the separation tank 3 is provided with a carrier liquid outlet 5 through which the carrier liquid flows out.
また分離槽３の下端３ａには再生濾材排出用及び抵抗部
材としての挿入管６を連続して垂下形成していろ。Further, an insertion tube 6 for discharging the recycled filter medium and as a resistance member is continuously formed to hang down from the lower end 3a of the separation tank 3.
そして挿入管６を濾過槽３内の濾材層２０上面２０ａま
で挿入し、これにより分離槽３内の再生浦材２を挿入管
６を介して濾過槽３内の濾材層２０に連続するようにし
ていろ。Then, the insertion tube 6 is inserted up to the upper surface 20a of the filter layer 20 in the filtration tank 3, so that the recycled porcelain material 2 in the separation tank 3 is connected to the filter layer 20 in the filtration tank 3 through the insertion tube 6. Teiro.
一方、濾過槽１は下端に濾材を抜出すための濾材抜出口
７が設げられ、また下部に被処理液供給口８、上部に処
理液を外部に取出す処理液管１０がそれぞれ設けられて
いる。On the other hand, the filtration tank 1 is provided with a filter medium extraction port 7 at the lower end for extracting the filter medium, a treated liquid supply port 8 at the lower part, and a treated liquid pipe 10 for taking out the treated liquid to the outside at the upper part. There is.
また第２図に示す例では濾材層２０に埋設した果液スク
リーン９を用い、該スクリーン９に処理液管１０を接？
している。In the example shown in FIG. 2, a fruit juice screen 9 embedded in the filter medium layer 20 is used, and the processing liquid pipe 10 is connected to the screen 9.
are doing.
処理液管１０は濾過槽１より上方で分離槽３の搬送液出
口５より下方の適当な位置で大気圧下に開口１０ａする
。The processing liquid pipe 10 has an opening 10a under atmospheric pressure at a suitable position above the filtration tank 1 and below the conveyed liquid outlet 5 of the separation tank 3.
この様な装置において、被処理液供給口８からの被処理
液が処理され、それが分離槽３の出口５から排出される
のではなく、処理液管１０かも排出されるための条件は
、第１図を参照して、ＰＨ ３ ＞ＰＨ ２ ＝ ＰＨ
＋Ｐｆ１）０ ・・・・・・・・・（１）で表すこと
ができる。In such an apparatus, the conditions for processing the liquid to be treated from the liquid to be treated supply port 8 and discharging it not from the outlet 5 of the separation tank 3 but also from the treated liquid pipe 10 are as follows. With reference to FIG. 1, PH 3 > PH 2 = PH
+Pf1)0 It can be expressed as (1).
ここでＰＨ３は出口５におけろ位置水頭、ＰＨ２は分離
槽下端部３ａよりも高く、搬送液出口５よりも低いレベ
ルＬにおける位置水頭、Ｐ旧は処理液管１０の開口１０
ａにおける位置水頭、Ｐｆ１は処理液管１０による圧損
水頭である。Here, PH3 is the position head at the outlet 5, PH2 is the position head at level L which is higher than the lower end 3a of the separation tank and lower than the conveyed liquid outlet 5, and P is the position head at the opening 10 of the processing liquid pipe 10.
The position head at point a, Pf1, is the pressure loss head due to the processing liquid pipe 10.
（１）式の意味は被処理液のみが供給口８から導入され
、再生濱材を搬送する搬送液が供給口４から導入されな
い場合に、処理液管１０から処理液が流出する状態で、
分離槽３内での水位が出口５よりも下のレベルＬにある
ことを意味する。The meaning of equation (1) is that when only the liquid to be treated is introduced from the supply port 8 and the carrier liquid for conveying the recycled beach material is not introduced from the supply port 4, the treatment liquid flows out from the treatment liquid pipe 10.
This means that the water level in the separation tank 3 is at a level L below the outlet 5.
すなわちそのようなレベルＬとなるよう処理液管１０の
開口位置１０ａを定めろわけである。That is, the opening position 10a of the processing liquid pipe 10 should be determined so that the level L is reached.
次に再生濾材供給口４から導入された搬送液が濾過槽１
の方へ行かずに出口５から排出されるための条件は、
ＰＨ３−ＰＨ２＜Ｐｆ ２＋Ｐｆ， ・・・・・
・・・・（２）で表すことができる。Next, the carrier liquid introduced from the regenerated filter medium supply port 4 is transferred to the filter tank 1.
The conditions for being discharged from exit 5 without going towards PH3-PH2<Pf 2+Pf, ...
...It can be expressed as (2).
ここでＰＨ３，ＰＨ２，Ｐｆは前記（１）式の場合と同
じである。Here, PH3, PH2, and Pf are the same as in the case of formula (1) above.
Ｐｆ２はレベルＬから挿入管６下端までの圧損水頭であ
る。Pf2 is the pressure loss head from the level L to the lower end of the insertion tube 6.
前記（１）式より
Ｐ −ＰＨＩ ＝Ｐｈ １ ＞Ｐｆ １ ・・・
・・・・・・（１）′Ｈ３
前記（２）式より
ＰＨ３ Ｐｕ２＝Ｐｈ２＜Ｐｆ２＋Ｐｆ１ ・・・・
・・（２）′を導くことができろ。From the above formula (1), P - PHI = Ph 1 > Pf 1 ...
......(1)'H3 From the above formula (2), PH3 Pu2=Ph2<Pf2+Pf1...
...(2) Be able to derive '.
（１）′式の意味は処理液管１０の圧損水頭Ｐｆがその
開口１０ａ位置から出口５までの高さｈに相当する水頭
ｐｈより小さければよいことである。The meaning of equation (1)' is that the pressure loss head Pf of the processing liquid pipe 10 should be smaller than the head ph corresponding to the height h from the opening 10a position to the outlet 5.
すなわち、その様な位置に、開口１０ａ位置を定めれば
よいのである。That is, the opening 10a position may be determined at such a position.
（２）′式は高さｈ２に相当する位置水頭Ｐｈ２が、レ
ベルＬにある液が．分離槽３から濾過槽１に入り、さら
に処理管１０から排出されるまでの全圧損水頭Ｐｆ２＋
Ｐｆ，よりも小さければよいという意味である。Equation (2)' shows that the liquid at level L has a position head Ph2 corresponding to height h2. Total pressure loss head Pf2+ from separation tank 3 to filtration tank 1 and further to discharge from processing pipe 10
This means that it should be smaller than Pf.
この（１）’，（２）′式を総合して定性的にいえば、
分離槽３の挿入管６を抵抗部材として前記Ｐｆ２を大き
くして？き、且つｈ２がＯ以上の小さい値となるよう処
理管１０の高さを定めれば目的が達成できるわけである
。Qualitatively speaking, combining these equations (1)' and (2)',
By using the insertion tube 6 of the separation tank 3 as a resistance member and increasing the Pf2? The purpose can be achieved by determining the height of the processing tube 10 so that h2 is a small value of 0 or more.
従って、現実的には操業時の変動を考慮した余裕α（正
の高さ）を見込んで ．
ｐ（ｈ１−α）＝Ｐｆ１
すなわち、Ｐｈ，＝Ｐｆ，＋Ｐα（Ｐαは余裕αに相当
する位置水頭）となるよう処理液管１０を出口５から距
離ｈよりさらに少し低い位置で開口１０ａすればよい。Therefore, realistically, a margin α (positive height) should be taken into account to account for fluctuations during operation. p(h1-α)=Pf1 That is, if the opening 10a of the processing liquid pipe 10 is opened at a position slightly lower than the distance h from the outlet 5 so that Ph, = Pf, +Pα (Pα is the position head corresponding to the margin α). good.
勿論理論的には前記した（１），（２）の式或いは（１
）’ ，（２）’の式の条件を満足するように処理液
管１０の開口１０ａ位置等を設定すればよい。Of course, theoretically, the above equations (1) and (2) or (1
)', the position of the opening 10a of the processing liquid pipe 10, etc. may be set so as to satisfy the conditions of the equation (2)'.
この様な条件は処理液管１０の圧損、挿入管６０寸法、
分離槽３０寸法、等を考慮することにより、処理液管１
０の開口１０ａ位置を比較的大きな範囲内で設定するこ
とができるものである。These conditions include the pressure loss of the processing liquid pipe 10, the dimensions of the insertion pipe 60,
By considering the dimensions of the separation tank 30, etc., the processing liquid pipe 1
The position of the opening 10a at 0 can be set within a relatively large range.
本発明は以上の様な構成としたので、濾過槽１内で処理
液は処理液管１０からのみ外部に排出され、一方、ＳＳ
等を含んで再生濾材供給口４から供給された搬送液は濾
過槽１へ移行することなく搬送液出口５から排出される
。Since the present invention has the above configuration, the processing liquid in the filtration tank 1 is discharged to the outside only from the processing liquid pipe 10, while the SS
The carrier liquid supplied from the regenerated filter medium supply port 4 including the regenerated filter medium is discharged from the carrier liquid outlet 5 without transferring to the filtration tank 1.
それ故、本発明は濾過槽１の上に分離槽３を併設した上
向流移動層式濾過装置において、複雑な設備を付加する
ことなく、また占有面積を増大させる様なこともなく、
処理液の品質を高度に保つことができるのである。Therefore, the present invention provides an upward flow moving bed type filtration device in which a separation tank 3 is installed above a filtration tank 1, without adding complicated equipment or increasing the occupied area.
This allows the quality of the processing liquid to be maintained at a high level.
なお、集液器９を濾材中に埋没した構造のものは、果液
器９が濾材の膨脹、流動化を抑えて良好な濾材状態を保
持する効果がある。In addition, in the structure in which the liquid collector 9 is embedded in the filter medium, the fruit juice container 9 has the effect of suppressing the expansion and fluidization of the filter medium and maintaining a good condition of the filter medium.
次に、本発明装置による濾過を実例について説明する。Next, an example of filtration by the apparatus of the present invention will be described.
第１図に示すように、内径６００ｍの濾過槽の上端に内
径３００ｍｍの分離槽を付設し、分離槽の下端部に内径
約５０ｍｍ、長さ６００ｗｒＬの挿入管６を連続して形
成して、この挿入管６を濾過槽１内の濾材層２０上面ま
で挿入した形とする。As shown in FIG. 1, a separation tank with an inner diameter of 300 mm is attached to the upper end of a filtration tank with an inner diameter of 600 m, and an insertion tube 6 with an inner diameter of about 50 mm and a length of 600 wrL is continuously formed at the lower end of the separation tank. This insertion tube 6 is inserted into the filter tank 1 up to the upper surface of the filter medium layer 20.
分離槽の上部には搬送液流出管１１の一端を開口させて
搬送液出口５とし、また、濱過槽上部の果液スクリーン
から処理液管を一部直立させて上方に導き、搬送液出口
位置よりｈ−２０ｃｒｎ下方の位置でサイフォンブレー
ク管１２に連結し、大気圧下に開口させた。At the top of the separation tank, one end of the conveyed liquid outflow pipe 11 is opened to serve as the conveyed liquid outlet 5, and a part of the processing liquid pipe is made upright from the fruit juice screen at the top of the filtering tank and guided upward to form the conveyed liquid outlet. It was connected to the siphon break pipe 12 at a position h-20crn below the position and opened under atmospheric pressure.
濾過槽下端の濾材抜出し口より３０分間に１回の割合で
濾材１０ｔを抜出し、その濾材が捕捉したＳＳの約９０
％を洗滌除去し、再生した濾材を同じく３０分を１サイ
クルとして、ＳＳ濃度０．５ｐｐｍの処理液１００ｔを
搬送液に用い、１．５分間で分離槽中段の再生濾材供給
口から分離槽に供給した。10 tons of filter media is extracted from the filter media outlet at the bottom of the filter tank once every 30 minutes, and approximately 90 tons of SS captured by the filter media is removed from the filter media outlet at the bottom of the filter tank.
% was washed away and the regenerated filter medium was transferred from the regenerated filter medium supply port in the middle of the separation tank to the separation tank in 1.5 minutes using 100 tons of treated liquid with an SS concentration of 0.5 ppm as the transport liquid, with one cycle of 30 minutes. supplied.
この場合、分離槽に入る搬送液のＳＳ濃度は約２５ｐｐ
ｍであった。In this case, the SS concentration of the carrier liquid entering the separation tank is approximately 25 pp.
It was m.
濾過槽下部の被処理液供給口からＳＳ濃度約１０ｐｐｍ
の被処理液を５ ．６ ｍ３／ ｈの流量で濾過槽に供
給したところ、ＳＳ濃度０．５ｐｐｍ の処理液が測
定誤差範囲内で被処理液供給量と同じ流量で得られた。SS concentration is approximately 10 ppm from the treated liquid supply port at the bottom of the filtration tank.
5. When supplied to the filtration tank at a flow rate of 6 m3/h, a treated liquid with an SS concentration of 0.5 ppm was obtained at the same flow rate as the supplied liquid to be treated, within the measurement error range.
この場合、処理液管の圧力損失は１５ｃｍ水柱であるか
ら、処理液管開口位置を定めるにあたり５ｃｍの余裕α
を見込んだものである。In this case, the pressure loss of the processing liquid pipe is 15 cm of water column, so when determining the opening position of the processing liquid pipe, there is a margin of 5 cm α.
This is in anticipation of.
仮に、ＳＳ濃度２ ５ ｐ ｐｍの搬送液が全量処理液
と混り合えば、処理液のＳＳ濃度は理論上、ｌｐｐｍ以
上となるから、濾過槽における被処理液のＳＳ除去率が
１００％であっても、搬送水の混入により、全体として
のＳＳ除去率は９０係以下に低下する。If the conveyed liquid with an SS concentration of 25 ppm is mixed with the entire treatment liquid, the SS concentration in the treatment liquid will theoretically be 1 ppm or more, so the SS removal rate of the treated liquid in the filtration tank will be 100%. Even if there is, the overall SS removal rate will drop to below 90% due to the contamination of the conveyed water.
以上により、本発明の装置によれば、ＳＳ濃度２ ５
ｐ ｐｍの搬送液により再生浦材を分離槽に供給しても
、ＳＳ濃度０．５ｐｐｍの処理液が被処理液供給量と同
量得られろことから、処理液と搬送液とが実質的に相互
に殆んど混り合わないことが確認される。As described above, according to the apparatus of the present invention, the SS concentration is 2 5
Even if the recycled porcelain material is supplied to the separation tank using a transport liquid with a concentration of 0.5 ppm, the same amount of treatment liquid with an SS concentration of 0.5 ppm as the supplied amount of the treated liquid will be obtained. It is confirmed that there is almost no mixing with each other.
第１図は本発明装置の一実施例を示す略縦断面図、第２
図は別の実施例を示す略縦断面図である。
１・・・・・・濾過槽、２・・・・・・再生濾材、３・
・・・・・分離槽、４・・・・・・再生濾材供給口、５
・・・・・・搬送液出口、６・・・・・・挿入管、７・
・・・・・濾材抜出し口、８・・・・・・被処理液供給
口、９・・・・・・集液器、１０・・・・・・処理液管
、１０ａ・・・・・・処理液管開口部、ｈ・・・・・・
処理液を果液位置から処理液管所定開口位置に導く際の
圧力損失にほぼ相当するヘッド差。Fig. 1 is a schematic vertical sectional view showing one embodiment of the device of the present invention;
The figure is a schematic vertical sectional view showing another embodiment. 1...Filter tank, 2...Regenerated filter medium, 3.
... Separation tank, 4 ... Regenerated filter media supply port, 5
...Transported liquid outlet, 6...Insertion tube, 7.
...Filtering medium outlet, 8...Processed liquid supply port, 9...Liquid collector, 10...Processing liquid pipe, 10a...・Processing liquid pipe opening, h...
The head difference is approximately equivalent to the pressure loss when guiding the processing liquid from the fruit juice position to the specified opening position of the processing liquid pipe.
Claims (1)
被処理液を導入して瀘過槽上部より処理液として外部へ
取出すようにした上向流移動層式濾過装置において、濾
過槽１の上に、搬送されてきた再生濾材とその搬送液と
を分離する分離槽３を併設すると共に、その分離槽下端
部３ａに連続して形成した再生濾材排出用及び抵抗部材
としての挿入管６を前記濾過槽１内の濾材層２０上面２
０ａまで挿入して分離槽３内の再生濾材２を挿入管６を
介して濾過槽１内の濱材層に連続させ、前記分離槽３の
略中段部に再生濾材を搬送液と共に分離槽３に供給する
再生濾材供給口４を、分離槽３の上部に前記搬送液を分
離槽３から流出させる搬送液出口５をそれぞれ設け、一
方、上記濾過槽１の上部から処理液を外部に取出す処理
液管１０を濾過槽１より上方で前記搬送液出口５よりも
ｈ１（ｈｌ＞Ｏ）だけ低い位置で大気圧下に開口１０ａ
することにより、該処理液管１０の開口位置におげる位
置水頭と管１０内での圧損水頭との和が前記分離槽下端
部３ａよりも高く且つ搬送液出口５よりもｈｚ（ｈｚ＞
０）だげ低いレベルＬに相当する位置水頭になるように
すると共に、該ｈ２に相当する位置水頭が前記レベルＬ
から挿入管６下端までの圧損水頭と処理液管１０の圧損
水頭との和よりも低くなるようにしたことを特徴とする
上向流移動層式濾過装置。1 In an upward flow moving bed type filtration device in which a liquid to be treated is introduced from the lower part of the filtration tank and taken out as a treated liquid from the upper part of the filtration tank while moving the particulate filter medium downward, the filtration tank 1 is At the top, a separation tank 3 for separating the transported recycled filter medium and its conveyed liquid is installed, and an insertion pipe 6 for discharging the recycled filter medium and as a resistance member is formed continuously at the lower end 3a of the separation tank. Upper surface 2 of the filter medium layer 20 in the filter tank 1
0a, the regenerated filter medium 2 in the separation tank 3 is connected to the shore material layer in the filtration tank 1 through the insertion tube 6, and the regenerated filter medium is inserted into the separation tank 3 together with the conveyed liquid in the approximately middle part of the separation tank 3. A regenerated filter media supply port 4 is provided at the top of the separation tank 3, and a transport liquid outlet 5 is provided at the top of the separation tank 3 to allow the transport liquid to flow out from the separation tank 3. On the other hand, the processing liquid is taken out from the top of the filtration tank 1 to the outside. The liquid pipe 10 is opened 10a under atmospheric pressure at a position above the filtration tank 1 and lower than the conveyed liquid outlet 5 by h1 (hl>O).
By doing so, the sum of the position head at the opening position of the processing liquid pipe 10 and the pressure loss head within the pipe 10 is higher than the lower end 3a of the separation tank and hz (hz>
0) At the same time, the position head corresponding to h2 is made to be the position head corresponding to the lower level L, and the position head corresponding to the level L
An upward flow moving bed type filtration device characterized in that the pressure loss head is lower than the sum of the pressure loss head from the to the lower end of the insertion tube 6 and the pressure loss head of the treated liquid pipe 10.
Priority Applications (6)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP52122170A JPS597485B2 (en) | 1977-10-11 | 1977-10-11 | Upflow moving bed filtration device |
| GB53955/77A GB1555918A (en) | 1976-12-29 | 1977-12-28 | Method and apparatus for the purification of liquid |
| DE19772758400 DE2758400A1 (en) | 1976-12-29 | 1977-12-28 | METHOD AND DEVICE FOR CLEANING A FLOW CAPABLE MEDIUM WITH A CLEANING AGENT |
| CH1622977A CH637030A5 (en) | 1976-12-29 | 1977-12-29 | Process and apparatus for purifying a liquid by countercurrent contact between this liquid and a purifying agent |
| NLAANVRAGE7714541,A NL184600C (en) | 1976-12-29 | 1977-12-29 | Apparatus for purifying a liquid with a particulate purification material in countercurrent and for regenerating the purification material. |
| FR7739720A FR2375888A1 (en) | 1976-12-29 | 1977-12-29 | COUNTER-CURRENT LIQUID-SOLID CONTACT DEVICE |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP52122170A JPS597485B2 (en) | 1977-10-11 | 1977-10-11 | Upflow moving bed filtration device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS5455868A JPS5455868A (en) | 1979-05-04 |
| JPS597485B2 true JPS597485B2 (en) | 1984-02-18 |
Family
ID=14829302
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP52122170A Expired JPS597485B2 (en) | 1976-12-29 | 1977-10-11 | Upflow moving bed filtration device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS597485B2 (en) |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5217250U (en) * | 1976-03-11 | 1977-02-07 |
-
1977
- 1977-10-11 JP JP52122170A patent/JPS597485B2/en not_active Expired
Also Published As
| Publication number | Publication date |
|---|---|
| JPS5455868A (en) | 1979-05-04 |
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