JP4936783B2 - Filtration concentrator - Google Patents
Filtration concentrator Download PDFInfo
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- JP4936783B2 JP4936783B2 JP2006125783A JP2006125783A JP4936783B2 JP 4936783 B2 JP4936783 B2 JP 4936783B2 JP 2006125783 A JP2006125783 A JP 2006125783A JP 2006125783 A JP2006125783 A JP 2006125783A JP 4936783 B2 JP4936783 B2 JP 4936783B2
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- 238000001914 filtration Methods 0.000 title claims description 117
- 239000010802 sludge Substances 0.000 claims description 88
- 239000012528 membrane Substances 0.000 claims description 64
- 238000005507 spraying Methods 0.000 claims 1
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 31
- 239000000706 filtrate Substances 0.000 description 12
- 238000010586 diagram Methods 0.000 description 5
- 238000009825 accumulation Methods 0.000 description 4
- 238000007664 blowing Methods 0.000 description 3
- 238000007599 discharging Methods 0.000 description 3
- 230000005484 gravity Effects 0.000 description 3
- 238000000034 method Methods 0.000 description 3
- 238000009958 sewing Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 230000018044 dehydration Effects 0.000 description 2
- 238000006297 dehydration reaction Methods 0.000 description 2
- 239000008213 purified water Substances 0.000 description 2
- 238000004062 sedimentation Methods 0.000 description 2
- 239000010865 sewage Substances 0.000 description 2
- 229910001220 stainless steel Inorganic materials 0.000 description 2
- 239000010935 stainless steel Substances 0.000 description 2
- 239000008399 tap water Substances 0.000 description 2
- 235000020679 tap water Nutrition 0.000 description 2
- 108090000862 Ion Channels Proteins 0.000 description 1
- 102000004310 Ion Channels Human genes 0.000 description 1
- 239000004677 Nylon Substances 0.000 description 1
- BZHJMEDXRYGGRV-UHFFFAOYSA-N Vinyl chloride Chemical compound ClC=C BZHJMEDXRYGGRV-UHFFFAOYSA-N 0.000 description 1
- 238000010521 absorption reaction Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 239000002184 metal Substances 0.000 description 1
- 229920001778 nylon Polymers 0.000 description 1
- 239000011148 porous material Substances 0.000 description 1
- 238000003825 pressing Methods 0.000 description 1
- 238000000746 purification Methods 0.000 description 1
- 238000003466 welding Methods 0.000 description 1
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Treatment Of Sludge (AREA)
Description
本発明は、浄水場や下水処理場等における汚泥の濾過濃縮装置の濾過板に関する。 The present invention relates to a filter plate of a sludge filtration and concentration device in a water purification plant, a sewage treatment plant, or the like.
浄水場や下水処理場から排出される汚泥は９０%以上の水分が含まれているので、従来は、一旦、重力沈降槽で濃縮した後、機械脱水を行って含水率８０%以下の濃縮汚泥とし、この濃縮汚泥を焼却、埋立て処分している。
従来の重力沈降槽による汚泥濃縮では、滞留時間が長く、汚泥の性状により含水率が大幅に変わるので、機械脱水を安定的に運転することが難しい問題点があった。そこで、重力沈降槽の代替手段として濾過濃縮装置が開発された。
Since sludge discharged from water treatment plants and sewage treatment plants contains 90% or more of moisture, conventionally, after concentration in a gravity sedimentation tank, mechanical dehydration is performed, and concentrated sludge with a moisture content of 80% or less. The concentrated sludge is incinerated and disposed of in landfills.
In the conventional sludge concentration in the gravity settling tank, the residence time is long and the moisture content varies greatly depending on the properties of the sludge. Therefore, it is difficult to stably operate the mechanical dehydration. Therefore, a filtration and concentration device was developed as an alternative to the gravity sedimentation tank.
従来の濾過濃縮装置について図１０を用いて説明する。従来の濾過濃縮装置は、底部がテーパー状に細くなっている汚泥槽１と、汚泥槽１に原汚泥を供給する配管と弁８とポンプ２と、汚泥槽１に原汚泥を供給する際にポンプ２を作動させて所定の水位まで汚泥を入れるために汚泥水位を検出する水位計１８と、汚泥槽１の下部に濃縮された後の濃縮汚泥を排出する配管および弁９と、汚泥槽１内に複数配置した濾過板３と、濾過板３で濾過された濾液を排出する濾液排出管４と、そして、濾液排出管４の途中に接続した給水タンク５と、給水タンク５に水を供給する水道水供給管６および弁１２と、給水タンク５に溜まった空気を排出する配管および弁１４と、加圧空気を供給するために給水タンク５に接続されたコンプレッサー７と弁１３とを備えている。濾液排出管４の出口高さは、濾過板３下端より下になるように設置している。また、濾過板３は、濾液と汚泥を隔離する濾過膜３ａと、濾過膜３ａを支持する濾枠３ｂから成っている。 A conventional filtration concentration apparatus will be described with reference to FIG. When a conventional filtration and concentration apparatus supplies sludge tank 1 having a tapered bottom, piping for supplying raw sludge to sludge tank 1, valve 8, pump 2, and sludge tank 1 for supplying raw sludge. A water level meter 18 that detects the sludge water level to activate the pump 2 and put sludge to a predetermined water level, a pipe and valve 9 for discharging the concentrated sludge after being concentrated at the bottom of the sludge tank 1, and the sludge tank 1 A plurality of filter plates 3 disposed therein, a filtrate discharge pipe 4 for discharging the filtrate filtered by the filter plate 3, a water supply tank 5 connected in the middle of the filtrate discharge pipe 4, and water is supplied to the water supply tank 5 A tap water supply pipe 6 and a valve 12, a pipe and valve 14 for discharging air accumulated in the water supply tank 5, and a compressor 7 and a valve 13 connected to the water supply tank 5 for supplying pressurized air. ing. The outlet height of the filtrate discharge pipe 4 is set to be lower than the lower end of the filter plate 3. The filter plate 3 includes a filter membrane 3a that separates the filtrate and sludge, and a filter frame 3b that supports the filter membrane 3a.
図１１は濾過板３の構成を示した図である。濾過板３の内側上部には、濾液の吸引や濃縮汚泥を剥離するための空気分配管１５が設けられている。この空気分配管１５は、金属や塩化ビニールなどの丸型や角型パイプを水平方向に設置し、パイプの下部に鉛直下方向に孔１６を複数設けている。孔１６は、濾過板３内部の濾液を吸引するためや、濃縮汚泥を濾過膜３aから剥離させる加圧空気を供給するために設けられている。空気分配管１５の加圧空気吹き込み口の反対側の端は、封止されている。 FIG. 11 is a diagram showing the configuration of the filter plate 3. An air distribution pipe 15 is provided on the inner upper part of the filter plate 3 for sucking the filtrate and peeling the concentrated sludge. The air distribution pipe 15 is a round or square pipe made of metal, vinyl chloride, or the like installed in the horizontal direction, and a plurality of holes 16 are provided vertically downward at the bottom of the pipe. The holes 16 are provided for sucking the filtrate inside the filter plate 3 and for supplying pressurized air for separating the concentrated sludge from the filter membrane 3a. The end of the air distribution pipe 15 opposite to the pressurized air blowing port is sealed.
次に、従来の濾過濃縮装置の運転方法を説明する。弁９〜１４はすべて閉じ、弁８は開けておく。そして、ポンプ２を作動させて、汚泥槽１に設置した濾過板３が水没する所定水位まで原汚泥を供給する。
次に、弁１２，１４を開いて給水タンク５が所定水位になるまで水を供給後、弁１２，１４を閉じる。そして、弁１０，１１を開いて濾過を開始する。濾過処理中は原汚泥の水位がこの所定水位を維持するようにポンプ２を作動させる。濾過膜３aに堆積する汚泥の厚さが、好ましくは１０〜１３ｍｍになるまで汚泥の供給および濾過を継続する。濾過を継続する時間は、予め汚泥堆積厚さと濾過時間の関係を調べておき、その後は、汚泥堆積厚さが前記１０〜１３ｍｍになる濾過時間を指標にして実施してもよい。例えば、このサイフォン濾過の場合は、９０分間濾過を行う。
Next, the operation method of the conventional filtration concentration apparatus will be described. Valves 9-14 are all closed and valve 8 is open. Then, the pump 2 is operated to supply the raw sludge to a predetermined water level where the filter plate 3 installed in the sludge tank 1 is submerged.
Next, after the valves 12 and 14 are opened and water is supplied until the water supply tank 5 reaches a predetermined water level, the valves 12 and 14 are closed. Then, the valves 10 and 11 are opened to start filtration. During the filtration process, the pump 2 is operated so that the water level of the raw sludge maintains this predetermined water level. The supply and filtration of the sludge is continued until the thickness of the sludge deposited on the filtration membrane 3a is preferably 10 to 13 mm. The time for which the filtration is continued may be carried out by examining the relationship between the sludge accumulation thickness and the filtration time in advance, and thereafter using the filtration time when the sludge accumulation thickness is 10 to 13 mm as an index. For example, in the case of this siphon filtration, filtration is performed for 90 minutes.
次に、弁１０を閉じ、弁８を開け、ポンプ２を作動させて、濾過膜３ａ表面に付着されなかった未濃縮汚泥を汚泥槽１から排出する。未濃縮汚泥を汚泥槽１から排出後、弁８を閉じる。
次に、弁１０，１３を開け、濾過膜３aの２次側に空気をコンプレッサー７で入れて加圧する。これにより、給水タンク５および濾液排出配管内の水とコンプレッサー７の空気を混合させた状態で、濾過膜３ａの１次側表面に付着した濃縮汚泥を濾過膜３ａから剥離および落下させ、剥離した濃縮汚泥を汚泥槽１の底に堆積させる。そして、弁９を開けて濃縮汚泥を汚泥槽１から排出する。
Next, the valve 10 is closed, the valve 8 is opened, the pump 2 is operated, and unconcentrated sludge that has not adhered to the surface of the filtration membrane 3 a is discharged from the sludge tank 1. After unconcentrated sludge is discharged from the sludge tank 1, the valve 8 is closed.
Next, the valves 10 and 13 are opened, and air is introduced into the secondary side of the filtration membrane 3a by the compressor 7 and pressurized. As a result, in the state where the water in the water supply tank 5 and the filtrate discharge pipe and the air of the compressor 7 are mixed, the concentrated sludge adhering to the primary side surface of the filtration membrane 3a is peeled off and dropped from the filtration membrane 3a. The concentrated sludge is deposited on the bottom of the sludge tank 1. Then, the valve 9 is opened to discharge the concentrated sludge from the sludge tank 1.
以上の濾過板を用いた濃縮汚泥剥離原理をまとめると以下の通りである。
・ 空気分配管１５に供給された加圧空気は、分配管に設けられた孔１６から濃縮汚泥が付着した濾過膜３aの２次側に向けて噴出する（一部は濾過膜流路に供給される）。これにより、空気分配管周辺の濾過膜３a表面に付着した濃縮汚泥は剥離する。
・ 剥離した濃縮汚泥は、汚泥槽１下部に向かって、他の濃縮汚泥を巻き込みながら、落下する。
The pressurized air supplied to the air distribution pipe 15 is ejected from the hole 16 provided in the distribution pipe toward the secondary side of the filtration membrane 3a to which the concentrated sludge has adhered (partly supplied to the filtration membrane channel) ) Thereby, the concentrated sludge adhering to the surface of the filtration membrane 3a around the air distribution pipe is peeled off.
-The peeled concentrated sludge falls toward the bottom of the sludge tank 1 while entraining other concentrated sludge.
従来の空気分配管を備えた濾過濃縮装置は、濾過板上部に濃縮汚泥が残留するという問題があった。すると、時間当たりの汚泥処理量が低下する事や、濾過板の寿命期間が短くなる問題を生じていた。つまり、濾過サイクルを繰り返すと、前記汚泥残留箇所ではさらに濾過吸引するため濾過膜と濃縮汚泥の付着力が強くなり目詰まりを起こした。
そこで、本発明は、濾過板上部に濃縮汚泥が残留することを防止できる濾過濃縮装置を提供することを目的とする。
A conventional filtration and concentration apparatus provided with an air distribution pipe has a problem that concentrated sludge remains on the upper part of the filter plate. As a result, the amount of sludge treated per hour is reduced and the lifetime of the filter plate is shortened. In other words, when the filtration cycle was repeated, the portion where the sludge remained was filtered and sucked, so that the adhesion between the filtration membrane and the concentrated sludge became strong and clogging occurred.
Then, an object of this invention is to provide the filtration concentration apparatus which can prevent that concentrated sludge remains in the upper part of a filter plate.
上記の問題を解決するために、本発明は、以下の構成とした。
請求項１に記載の濾過濃縮装置は、汚泥を貯留する汚泥槽と、前記汚泥を濾過する濾過膜と、前記濾過膜により濃縮された濃縮汚泥を前記濾過膜から剥離させるための気体を前記濾過膜の２次側に供給する配管とを備えた濾過濃縮装置において、前記配管は、前記濾過膜上部の２次側に設置されるとともに、前記濾過膜の２次側の面が下方を向くように傾斜した該濾過膜の傾斜領域へ向けて噴出させる孔を備えている。ここで、前記傾斜領域とは、前記濾過膜が頭頂部付近の斜めに下降している前記濾過膜の領域のことである。なお、前記濾過膜の頭頂部が水平の場合は、前記傾斜領域に前記頭頂部の水平部分も含む。上記構成にすれば、管内に加えられた加圧空気は、濾過膜を下から上方向に圧力をかけることができ、前記傾斜領域に濃縮汚泥が残留することを防止できる。
In order to solve the above problems, the present invention has the following configuration.
The filtration concentration apparatus according to claim 1, wherein the sludge tank for storing sludge, the filtration membrane for filtering the sludge, and the gas for separating the concentrated sludge concentrated by the filtration membrane from the filtration membrane are filtered. in the filtration concentrator and a piping for supplying the secondary side of the membrane, the piping, as well is installed on the secondary side of the filtration membrane upper secondary-side surface of the filtration membrane downward A hole is provided for jetting toward the inclined region of the filtration membrane inclined so as to face . Here, the said inclination area | region is an area | region of the said filtration membrane in which the said filtration membrane descends diagonally in the head vicinity vicinity . In addition, when the top part of the said filtration membrane is horizontal, the horizontal part of the said top part is also included in the said inclination area | region. According to the above configuration, the pressurized air applied to the inside of the pipe can apply pressure from below to above the filtration membrane, and can prevent the concentrated sludge from remaining in the inclined region.
請求項２に記載の濾過濃縮装置は、請求項１に記載の濾過濃縮装置において、前記孔と前記濾過膜の間に空隙を設けている。上記構成にすれば、加圧空気が濾過膜に与える振動を広範囲に伝達することができる。
請求項３に記載の濾過濃縮装置は、請求項１または２に記載の濾過濃縮装置において、前記濾過膜は、柔軟性があるものを用いている。
A filtration concentration apparatus according to a second aspect is the filtration concentration apparatus according to the first aspect, wherein a gap is provided between the hole and the filtration membrane. If it is set as the said structure, the vibration which pressurized air gives to a filtration membrane can be transmitted in a wide range.
The filtration concentration apparatus according to claim 3 is the filtration concentration apparatus according to claim 1 or 2, wherein the filtration membrane is flexible.
請求項４に記載の濾過濃縮装置は、請求項１ないし３のいずれか１項に記載の濾過濃縮装置において、前記管と前記濾過膜の間に多孔質部材を設けている。上記構成にすれば、濾液および加圧空気の通流を容易にすることができる。
A filtration concentration apparatus according to a fourth aspect is the filtration concentration apparatus according to any one of the first to third aspects, wherein a porous member is provided between the tube and the filtration membrane. If it is the said structure, the flow of a filtrate and pressurized air can be made easy .
本発明によれば、濾過膜全面に付着した濃縮汚泥を剥離できるので、時間当たりの汚泥処理量の低下を防止できる。そして、濾過板上部に残留する濃縮汚泥がなくなることから、濾過膜の目詰まりが低減されるので、濾過膜の交換サイクルを長くすることができる。 According to the present invention, since the concentrated sludge adhering to the entire membrane surface can be peeled off, it is possible to prevent a decrease in the amount of sludge treated per hour. And since the concentrated sludge remaining on the upper part of the filter plate is eliminated, clogging of the filter membrane is reduced, so that the replacement cycle of the filter membrane can be lengthened.
以下、本発明の実施形態を実施例に基づき説明する。本実施例の濾過濃縮装置は、濾過板３を除いて、従来技術である図１０と同じ構成の濾過濃縮装置である。
図１は、本発明が適用される濾過板３の構成図である。濾過板３は、濾過膜３aと、空気分配管１５とを備える。必要に応じて図示しない濾枠３bを備えていても良い。濾過膜３aは、周囲を必要に応じてミシン糸で縫合して袋状になっている。さらに、濾過膜中央部は、ミシン糸で縫合して濾過膜流路を形成されている。濾過膜３aを縫合した袋内部には、濾過膜表面に付着した濃縮汚泥の水分を吸引するため、また、濃縮汚泥を剥離するための加圧空気が流れる空気分配管１５が設けられている。本実施例の空気分配管１５のA−A断面図を図２に示す。空気分配管１５には、濾過膜３a上部の傾斜領域へ空気を噴出させる孔を備えている。空気分配管１５の加圧空気吹き込み口の反対側の端は、封止されている。
Hereinafter, embodiments of the present invention will be described based on examples. The filtration concentration apparatus of the present embodiment is a filtration concentration apparatus having the same configuration as that of FIG.
FIG. 1 is a configuration diagram of a filter plate 3 to which the present invention is applied. The filter plate 3 includes a filter membrane 3 a and an air distribution pipe 15. You may provide the filter frame 3b which is not shown in figure as needed. The filtration membrane 3a is formed into a bag shape by sewing the periphery with a sewing thread as necessary. Further, the central portion of the filtration membrane is sewn with a sewing thread to form a filtration membrane flow path. An air distribution pipe 15 through which pressurized air for sucking the moisture of the concentrated sludge adhering to the surface of the filtration membrane and for removing the concentrated sludge flows is provided inside the bag to which the filtration membrane 3a is stitched. FIG. 2 shows an AA cross-sectional view of the air distribution pipe 15 of the present embodiment. The air distribution pipe 15 is provided with a hole for ejecting air to the inclined area above the filtration membrane 3a. The end of the air distribution pipe 15 opposite to the pressurized air blowing port is sealed.
本実施例の濾過濃縮装置の運転方法は、前述の従来技術の濾過濃縮装置における運転方法と同じである。弁９〜１４はすべて閉じ、弁８は開けておく。そして、ポンプ２を作動させて、汚泥槽１に設置した濾過板３が水没する所定水位まで原汚泥を供給する。
次に、弁１２，１４を開いて給水タンク５が所定水位になるまで水を供給後、弁１２，１４を閉じる。そして、弁１０，１１を開いて濾過を開始する。濾過処理中は原汚泥の水位がこの所定水位を維持するようにポンプ２を作動させる。濾過膜３aに堆積する汚泥の厚さが、好ましくは１０〜１３ｍｍになるまで汚泥の供給および濾過を継続する。濾過を継続する時間は、予め汚泥堆積厚さと濾過時間の関係を調べておき、その後は、汚泥堆積厚さが前記１０〜１３ｍｍになる濾過時間を指標にして実施してもよい。例えば、このサイフォン濾過の場合は、９０分間濾過を行う。
The operation method of the filtration concentration apparatus of the present embodiment is the same as the operation method in the above-described conventional filtration concentration apparatus. Valves 9-14 are all closed and valve 8 is open. Then, the pump 2 is operated to supply the raw sludge to a predetermined water level where the filter plate 3 installed in the sludge tank 1 is submerged.
Next, after the valves 12 and 14 are opened and water is supplied until the water supply tank 5 reaches a predetermined water level, the valves 12 and 14 are closed. Then, the valves 10 and 11 are opened to start filtration. During the filtration process, the pump 2 is operated so that the water level of the raw sludge maintains this predetermined water level. The supply and filtration of the sludge is continued until the thickness of the sludge deposited on the filtration membrane 3a is preferably 10 to 13 mm. The time for which the filtration is continued may be carried out by examining the relationship between the sludge accumulation thickness and the filtration time in advance, and thereafter using the filtration time when the sludge accumulation thickness is 10 to 13 mm as an index. For example, in the case of this siphon filtration, filtration is performed for 90 minutes.
次に、弁１０を閉じ、弁８を開け、ポンプ２を作動させて、濾過膜３ａ表面に付着されなかった未濃縮汚泥を汚泥槽１から排出する。未濃縮汚泥を汚泥槽１から排出後、弁８を閉じる。
次に、弁１１，１４を開けた状態にして吸水タンク５および濾液排出配管４の水を除いた後、弁１１，１４を閉じる。
Next, the valve 10 is closed, the valve 8 is opened, the pump 2 is operated, and unconcentrated sludge that has not adhered to the surface of the filtration membrane 3 a is discharged from the sludge tank 1. After unconcentrated sludge is discharged from the sludge tank 1, the valve 8 is closed.
Next, after the valves 11 and 14 are opened and the water in the water absorption tank 5 and the filtrate discharge pipe 4 is removed, the valves 11 and 14 are closed.
次に、弁１０，１３を開け、濾過膜３aの２次側に空気をコンプレッサー７で入れて加圧する。これにより、濾過膜３ａの１次側表面に付着した濃縮汚泥を濾過膜３ａから剥離および落下させ、剥離した濃縮汚泥を汚泥槽１の底に堆積させる。そして、弁９を開けて濃縮汚泥を汚泥槽１から排出する。
従来技術と本発明の実施例の結果を表１に示す。使用した汚泥は、水源がダム放流水、浄水処理量は2万ｍ３／日の浄水汚泥である。また、濾過は、濾過圧力−３３ｋＰａ、濾過時間９０分間で行った。濃縮汚泥剥離は、加圧空気圧力５ｋｇ／ｃｍ２、5秒間加圧継続した。濾過膜は、ナイロン製のモノフィラメントで、かつ、１枚当たり濾過面積１．３ｍ２のものを用いた。
表１の結果から、同じ濃縮汚泥厚さで、かつ、濃縮汚泥濃度の条件下において、空気分配管１５は、濾過膜３a上部の傾斜領域へ空気を噴出させる孔１６を備えたことによって、濃縮汚泥剥離率は、従来技術では６０〜９０％であったが、本発明の実施例では９５〜９８％に増加した。
Next, the valves 10 and 13 are opened, and air is introduced into the secondary side of the filtration membrane 3a by the compressor 7 and pressurized. Thereby, the concentrated sludge adhering to the primary side surface of the filtration membrane 3a is peeled and dropped from the filtration membrane 3a, and the peeled concentrated sludge is deposited on the bottom of the sludge tank 1. Then, the valve 9 is opened to discharge the concentrated sludge from the sludge tank 1.
The results of the prior art and the examples of the present invention are shown in Table 1. The sludge used is dam discharge water and the amount of purified water treated is 20,000 m 3 / day of purified water sludge. The filtration was performed at a filtration pressure of −33 kPa and a filtration time of 90 minutes. Concentrated sludge stripping was continued for 5 seconds under a pressurized air pressure of 5 kg / cm 2 . The filtration membrane used was a monofilament made of nylon and having a filtration area of 1.3 m 2 per sheet.
From the results shown in Table 1, the air distribution pipe 15 is provided with a hole 16 for injecting air into the inclined region above the filtration membrane 3a under the same concentrated sludge thickness and concentrated sludge concentration conditions. The sludge stripping rate was 60 to 90% in the prior art, but increased to 95 to 98% in the examples of the present invention.
図３は、濾過膜の傾斜面と鉛直のなす角を、４５度以下とする実施例である。濾過板３上部の剥離した濃縮汚泥が、まだ濾過膜に付着している濃縮汚泥を巻き込んで剥離するので、濾過膜から濃縮汚泥を剥離させることが容易になる。そして、空気分配管１５の鉛直方向断面形状を三角形とする場合においては、三角形の底辺部が広いと濾過板３の厚みが増し、濾過板３内に残留する濾液が増加するため、剥離後の濃縮汚泥濃度は低下する。よって、三角形の底辺が狭い形状とすることが望ましい。
FIG. 3 shows an embodiment in which the angle formed by the inclined surface of the filtration membrane and the vertical is 45 degrees or less. Since the concentrated sludge peeled off from the upper part of the filter plate 3 entrains and separates the concentrated sludge still adhering to the filtration membrane, it becomes easy to peel the concentrated sludge from the filtration membrane. And in the case where the vertical cross-sectional shape of the air distribution pipe 15 is a triangle, if the base of the triangle is wide, the thickness of the filter plate 3 increases and the filtrate remaining in the filter plate 3 increases. Concentrated sludge concentration decreases. Therefore, it is desirable that the triangle has a narrow base.
図４は、図２において、空気分配管１５と濾過膜３aの間に多孔質部材１９を設けた実施例である。多孔質材１９としては、メッシュ状のものが好ましい。
図５から図９は、孔１６と濾過膜３aの間に空隙を設けた実施例である。より具体的には、突出部１７を空気分配管１５の頭頂部に設けて、濾過膜３aと孔１６の間に空隙を設けている。図５は、図３において、空気分配管１５頭頂部に突出部１７を設けた実施例である。図６は、図２の空気分配管１５頭頂部を絞り、空気分配管１５頭頂部に突出部１７を設けた実施例である。図７，８の空気分配管１５は、ステンレス板に孔１６をあけ、図９のようにプレス加工で湾曲させて、２枚の前記ステンレス板を抱き合わせ、加圧空気吹き込み口を除く周囲を電気抵抗溶接して空気分配管１５を形成したものである。図９は、空気分配管１５から部分的に離隔させるように濾過膜３aを形成し、濾過後に濾過膜が２次側を下にして傾斜している濾過膜傾斜領域の下に孔１６が位置するようにした実施例である。すなわち、図９の実施例では、濾過膜３aは柔軟性を備えており、濾過前後で変形する。
FIG. 4 shows an embodiment in which a porous member 19 is provided between the air distribution pipe 15 and the filtration membrane 3a in FIG. As the porous material 19, a mesh-like material is preferable.
5 to 9 show an embodiment in which a gap is provided between the hole 16 and the filtration membrane 3a. More specifically, the protrusion 17 is provided at the top of the air distribution pipe 15, and a gap is provided between the filtration membrane 3 a and the hole 16. FIG. 5 shows an embodiment in which a protrusion 17 is provided on the top of the air distribution pipe 15 in FIG. FIG. 6 shows an embodiment in which the top of the air distribution pipe 15 shown in FIG. 2 is throttled and a protrusion 17 is provided on the top of the air distribution pipe 15. The air distribution pipe 15 shown in FIGS. 7 and 8 has a hole 16 formed in a stainless steel plate, and is curved by pressing as shown in FIG. 9 so that the two stainless steel plates are joined together and the surroundings except for the pressurized air blowing port are electrically connected. The air distribution pipe 15 is formed by resistance welding. In FIG. 9, the filtration membrane 3a is formed so as to be partially separated from the air distribution pipe 15, and the hole 16 is located under the filtration membrane inclined region where the filtration membrane is inclined with the secondary side down after filtration. This is an embodiment. That is, in the embodiment of FIG. 9, the filtration membrane 3a has flexibility and deforms before and after filtration.
１ 汚泥槽
２ ポンプ
３ 濾過板
３ａ 濾過膜
３ｂ 濾枠
４ 濾液排出管
５ 給水タンク
６ 水道水供給管
７ コンプレッサー
８〜１４ 弁
１５ 空気分配管
１６ 孔
１７ 突出部
１８ 水位計
１９ 多孔質部材
DESCRIPTION OF SYMBOLS 1 Sludge tank 2 Pump 3 Filter plate 3a Filtration membrane 3b Filter frame 4 Filtrate discharge pipe 5 Water supply tank 6 Tap water supply pipe 7 Compressor 8-14 Valve 15 Air distribution pipe 16 Hole 17 Protrusion 18 Water level gauge 19 Porous member
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| JPS61153120A (en) * | 1984-12-27 | 1986-07-11 | Fuji Electric Co Ltd | Method for fixing filter cloth of filter plate in filtration concentration device |
| JPS62262722A (en) * | 1986-05-08 | 1987-11-14 | Fuji Electric Co Ltd | Filter plate of filtration concentrator |
| JPS63270513A (en) * | 1987-04-27 | 1988-11-08 | Fuji Electric Co Ltd | Filter plate for filtration concentrating equipment |
| JPS63319012A (en) * | 1987-06-22 | 1988-12-27 | Ishigaki Kiko Kk | Method and device for filtration using coiled spring filter medium |
| JP2766959B2 (en) * | 1990-08-01 | 1998-06-18 | オルガノ株式会社 | Swelling filter |
| JP3119006B2 (en) * | 1993-01-07 | 2000-12-18 | 富士電機株式会社 | Filtration concentration device and filtration concentration method |
| FR2775911B1 (en) * | 1998-03-16 | 2000-07-21 | Suez Lyonnaise Des Eaux | IMPROVEMENTS IN SOLID-LIQUID SEPARATION EQUIPMENT, PARTICULARLY FOR THE BIOLOGICAL PURIFICATION OF WASTE WATER |
| JP2000246018A (en) * | 1999-03-03 | 2000-09-12 | Daicel Chem Ind Ltd | Flat membrane element |
| JP4267773B2 (en) * | 1999-08-18 | 2009-05-27 | オルガノ株式会社 | Sludge filtration dehydrator |
| JP4471702B2 (en) * | 2004-03-30 | 2010-06-02 | オルガノ株式会社 | Inflatable filter |
| JP4164498B2 (en) * | 2005-02-14 | 2008-10-15 | アマドック株式会社 | Filter body of siphon type filtration concentrator, method for manufacturing the filter body, filter plate of siphon type filter concentrator, and method for fixing filter body to support frame in the filter plate |
| JP2006289241A (en) * | 2005-04-08 | 2006-10-26 | Shinshu Univ | Dehydration method of sewage sludge, and its apparatus |
| JP4761043B2 (en) * | 2005-12-22 | 2011-08-31 | 国立大学法人信州大学 | Mud removal method and apparatus |
| JP4677374B2 (en) * | 2006-06-28 | 2011-04-27 | メタウォーター株式会社 | Filtration concentration apparatus and filtration concentration method |
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