【発明の詳細な説明】
産業上の利用分野
本発明は懸濁液の濃縮設備に関するものである．従来の
技術
１（Ｉｌｌ濁液、例えば汚泥を濃縮する従来の濃縮設備
としては槽本体内の上部に膜モジュールを配置し、この
下方に散気管を配設し，散気管に送風機を接続したもの
がある．槽本体内の汚泥は散気管より吹き出す仝気によ
り撹拌され、膜モジュールの近くを通過する際に、その
水分が強制的に吸引される．この結果、槽本体内の汚泥
は濃縮され、汚泥中のＳＳ（浮遊固形物）の含有率が高
められる．汚泥中のＳＳの濃度は，膜モジュールの透過
流速，が高いほど高めることができる．
発明が解決しようとするＩＩ題
しかし，上記従来の構成によれば、濃縮槽に入ってくる
原汚泥濃度は例えば０．６〜１％にもかかわらず濃縮槽
より出ていく濃縮汚泥の濃度は常に目標の値，例えば４
％まで高めなければならない，このことは、濃縮槽内の
汚泥濃度は絶えず濃縮処理目標値濃度，即ち４％にまで
高められた状態にあることを意味する．しかしながら，
一般に、膜モジュール（もしくは膜）の透過水量は対象
液中の懸濁物質の濃度に非常に高い相関関係を有し、そ
の濃度が高い程，透過水量は低くなる．即ち，従来の濃
縮槽は低い透過水量で運転していることにむり，結果と
して、膜モジュール本数も多く、かつその膜モジュール
を収納する濃縮槽も大きいものとなっていた．
本発明は上記ａＭを解決するもので歴濁液中のＳＳ濃度
を従来より高い透過水量で高めることができる闇濁液の
濃縮設備を提償することを目的とするものである．
課題を解決するための手段
上記課題を解決するために本発明は、恕濁液中の水を分
離するろ適用膜モジュールと、このろ適用膜モジュール
の下方に配置されて懸濁液を撹拌する散気管とを有する
ものをろ過用ユニット（槽部）とし、このろ過用ユニッ
トを処理規模に見合う数だけ、配置するのであるが、従
来のように１つの槽内で槽内の彼処理液が自由に混合し
ないように、いくつかのろ過用ユニットを単位に複数段
に仕切り，被処理｝ｌ！濁液は入口側（低濃度側）から
順次ろ過用ユニットで水分が引抜き（ろ過）濃縮されな
がら出口側（高濃度側）に送られ，最終的には処理目標
の憑濁液濃度となって取り出されるように構成したもの
である．
作用
従来の濃縮槽内の懸濁液濃度は前述のように濃縮槽から
の〃｝口濃度と等しく高いものであるためａ縮槽内での
膜の透過水量は低いが、本考案の上言己構或により彼処
理懸濁液は順次複数段の槽部に送られていきむから濃縮
作用（水の吸引）を受け、濃度を品められ最終段の槽部
では目標濃縮懸濁液濃度と々りａ縮懸濁液として取り出
されている．そのため本考案の感縮槽内の最終段の槽部
以外の槽部室内の懸濁液濃度は原懸濁液側（入口側）に
近い程厚１！ｌ濁液濃度に近く低いものとむっているた
め最終段の槽部以外の膜モジュールの透過水量は、従来
濃縮槽内の膜モジュールのフラックスよりは高く維持で
きるのみならず，かつ本考案の癩１ｌＩｊｆＩの原汚泥
入口側の槽部に近い程高く維持できる．
実施例
以下、本発明の一実施例を図面に基づいて説明する．
１５１図において、１は２段の汚泥濃縮設備で、第１お
よび第２の濃縮槽２．３が備えられ、これらの濃縮槽２
，３内にはそれぞれ上部に膜モジュ一゛ル４，５が設け
られているとともに各膜モジュール４，５の下方に散気
管６，７が配置されている．第工濃縮槽２の底部には、
ポンプ８が設けられた接続管９の一端が接続され、接続
管９の他端は第２の濃縮槽３内に開口されている．なお
、各膜モジュール４，５は弁１０．１１を有する接続管
１２．１３を介して吸引用ポンプ１４．１５に接続され
、１摸モジュール４，５を介して強制的に水が吸引され
る．また，各散気管６，７は弁１６，１７を有する償給
管１８．１９を介して１つの送風機２０に並列に接続さ
れ，空気が偶給されている．２１は第２ １ｆｌ４’！
？ ２の上部に取付けられた濃縮汚泥受けである．
上記構成において、第工の濃縮Ｍ２内に偶給された例え
ばＳＳがｌ％の汚泥ａは、散気管６からの空気により撹
拌され、膜モジュール４により水分が強制的に吸引され
る。これにより汚泥は例えばＳＳが２〜３％に濃縮され
る．濃縮された汚泥は、ボンプ８により第ｌの′ａ縮槽
２の底部より弓き出されて第２の濃縮槽３内に供給され
る。この濃縮汚泥は散気管７からの空気により撹拌され
，膜モジュール５によりさらに水分が強制的に吸引され
る．これにより汚泥はＳＳが目標値である４〜５％にな
るようにさらに濾縮され、ＳＳ１：ｌ’ｆｉ縮汚泥受け
２ｌから脱水装置々どへ送られる．なお、第↓および第
２の凛縮槽２，３の膜モジュール４，５から抜き出され
た水は放流される．また，上記実施例においては第ｌの
真縮槽２で濃縮された汚泥をボンプ８により第２の濃縮
槽３に供給する構成としたが，第１の濃縮槽２を第２の
濃縮槽３よりも高い位置に配置し，水位差により第２の
！Ｉ縮槽３に供給してもよい。DETAILED DESCRIPTION OF THE INVENTION Field of Industrial Application The present invention relates to equipment for concentrating suspensions. Conventional technology 1 (Ill) Conventional concentration equipment for concentrating turbid liquids, such as sludge, is one in which a membrane module is placed in the upper part of the tank body, an aeration pipe is arranged below this, and a blower is connected to the aeration pipe. The sludge in the tank body is stirred by the air blown out from the aeration pipe, and when it passes near the membrane module, the water is forcibly sucked in. As a result, the sludge in the tank body is concentrated. , the content of SS (suspended solids) in sludge is increased.The concentration of SS in sludge can be increased as the permeation flow rate of the membrane module increases. According to the conventional configuration, even though the concentration of raw sludge entering the thickening tank is, for example, 0.6 to 1%, the concentration of thickened sludge leaving the thickening tank is always the target value, for example, 4%.
This means that the sludge concentration in the thickening tank is constantly increased to the target value concentration for thickening treatment, that is, 4%. however,
Generally, the amount of water permeated through a membrane module (or membrane) has a very high correlation with the concentration of suspended solids in the target liquid, and the higher the concentration, the lower the amount of water permeated. In other words, conventional concentrators operate with a low permeate flow rate, resulting in a large number of membrane modules and a large concentrator to house the membrane modules. The present invention solves the aM problem described above, and aims to provide a dark liquid concentration facility that can increase the SS concentration in a dark liquid with a higher amount of permeated water than before. Means for Solving the Problems In order to solve the above problems, the present invention includes a filtration membrane module that separates water in a suspension, and a filter disposed below the filtration membrane module to agitate the suspension. The filtration unit (tank) is equipped with an aeration pipe, and the filtration units are arranged in a number commensurate with the processing scale. In order to prevent free mixing, several filtration units are divided into multiple stages, and the treated }l! The turbid liquid is sent to the outlet side (high concentration side) while being concentrated by a filtration unit, where water is sequentially extracted (filtered) from the inlet side (low concentration side), and finally the concentration of the turbid liquid reaches the treatment target. It is configured so that it can be taken out. Effect As mentioned above, the concentration of the suspension in the conventional thickening tank is as high as the concentration at the top of the thickening tank, so the amount of water that permeates through the membrane in the a-concentrating tank is low. Due to its own structure, the treated suspension is sequentially sent to multiple stages of tanks, receives a concentration effect (suction of water), improves its concentration, and reaches the target concentrated suspension concentration in the final stage tank. It is extracted as a liquid suspension. Therefore, the concentration of the suspension in the chambers other than the final stage tank in the condensation tank of the present invention is as thick as 1 as it is closer to the original suspension side (inlet side)! Since the flux is expected to be low and close to the concentration of the turbid liquid, the amount of permeated water in the membrane modules other than the final stage tank can not only be maintained higher than the flux of the membrane module in the conventional thickening tank, but also The closer the tank is to the raw sludge inlet side, the higher it can be maintained. EXAMPLE Hereinafter, an example of the present invention will be explained based on the drawings. In Figure 151, 1 is a two-stage sludge thickening facility, which is equipped with a first and second thickening tank 2.3.
, 3, membrane modules 4, 5 are provided at the upper part thereof, and diffuser pipes 6, 7 are arranged below each membrane module 4, 5. At the bottom of the first concentration tank 2,
One end of a connecting pipe 9 provided with the pump 8 is connected, and the other end of the connecting pipe 9 is opened into the second concentration tank 3. In addition, each membrane module 4, 5 is connected to a suction pump 14.15 via a connecting pipe 12.13 having a valve 10.11, and water is forcibly sucked through the first sample module 4, 5. ．． Further, each of the diffuser pipes 6 and 7 is connected in parallel to one blower 20 through compensation pipes 18 and 19 having valves 16 and 17, so that air is supplied in parallel. 21 is the second 1fl4'!
? This is a thickened sludge receiver attached to the top of 2. In the above configuration, the sludge a containing, for example, 1% SS, which is supplied into the concentrator M2 in the second step, is stirred by air from the aeration pipe 6, and water is forcibly sucked by the membrane module 4. As a result, the sludge is concentrated to, for example, 2 to 3% SS. The concentrated sludge is pumped out from the bottom of the l'a condensing tank 2 by the pump 8 and supplied into the second condensing tank 3. This thickened sludge is stirred by air from the aeration tube 7, and further water is forcibly sucked in by the membrane module 5. As a result, the sludge is further filtered so that the SS becomes the target value of 4 to 5%, and is sent from the SS1:l'fi reduced sludge receiver 2l to the dewatering equipment. Note that the water extracted from the membrane modules 4 and 5 of the ↓ and second refrigeration tanks 2 and 3 is discharged. Furthermore, in the above embodiment, the sludge concentrated in the first vacuum tank 2 is supplied to the second thickener tank 3 by the pump 8, but the first thickener tank 2 is connected to the second thickener tank 3. It is placed in a higher position than the second one due to the water level difference. It may also be supplied to the I-condensation tank 3.
第２図は本発明の他の実施例に係る２段仕切りａ縮設備
３５を示すもので、上記実施例と同じものには同じ番号
を付してその説明は省略する．この実施例においては工
つの濁縮Ｍ３０内が仕切壁３Ｉにより第上のｉｌｌ縮槽
部３２と第２の濃縮槽部３３とに分割され、第工のａ縮
槽部３２と第２の濃縮槽部３３とは仕切壁３ｌ下方の連
通部３４（上方連通部もしくはポンプを介しての辿通で
も可）を介して連通されている．
この構成によっても第↓の濃縮槽部３２において汚泥が
例えばＳＳａ度が２〜３％となるように濃縮され、さら
にこの濃縮汚泥は連通部３４を介して第２の濃縮槽部３
３内にａ（給されてＳＳＪＩ度が目標値である４〜６％
となるように濃縮される．なお，上記実施例においては
各サイドの膜モジュール４，５にそれぞれ吸引用ポンプ
１４，Ｉｓを亭妾続したが、１台の吸引用ポンプで両サ
イドの膜モジュール４．５から水を吸引するようにして
もよい．また、上記実施例においては２段の濃縮装置の
場合について示したが、ａ縮装置を３段以上に構或して
もよい．
発明の効果
以上のように本発明によれば、汚泥中のＳＳの濃度が目
標の値になるように＋Ｓ濁液を膜モジュールにより従来
より高い透過水量で濃縮することができるため、従来と
同じ規模の原Ｉｌ！ｌｌｌ濁液量に対しては少ない膜モ
ジュールで処理することができる。FIG. 2 shows a two-stage partition a-compression equipment 35 according to another embodiment of the present invention, and the same parts as in the above embodiment are given the same numbers and their explanation will be omitted. In this embodiment, the inside of the condensation chamber M30 is divided by a partition wall 3I into an upper ill condensation tank section 32 and a second condensation tank section 33. It is communicated with the tank 33 via a communication section 34 below the partition wall 3l (an upper communication section or passage via a pump is also possible). With this configuration as well, the sludge is concentrated in the ↓th thickening tank section 32 so that the SSa degree is, for example, 2 to 3%, and further, this thickened sludge is transferred to the second thickening tank section 3 through the communication section
A within 3 (the SSJI degree is the target value of 4-6%)
It is concentrated so that In the above embodiment, the suction pumps 14 and Is were connected to the membrane modules 4 and 5 on each side, respectively, but one suction pump sucks water from the membrane modules 4 and 5 on both sides. You can do it like this. Further, in the above embodiment, the case of a two-stage condensing device is shown, but the a-condensing device may be configured to have three or more stages. Effects of the Invention As described above, according to the present invention, +S turbidity can be concentrated using a membrane module with a higher amount of permeated water than before so that the concentration of SS in sludge reaches the target value. The origin of scale! It is possible to process 1000 ml of turbid liquid with a small number of membrane modules.
【図面の簡単な説明】[Brief explanation of drawings]
第１図は本発明の一実施例に係る濃縮設備を示す概酩図
、第２図は本発明の他の実施例に係る濃縮設備を示す概
略図である．
１，３５・・・濃縮設備、２・・・第１の濃縮槽（低真
度側Ｍｆｆｌ＋） 、３−．第２のａ！ｌｉ槽（高濃度
４１＋１１槽部），４，５・・・膜モジュール、６．７
・・・散気管、３２・・・第１の濃縮槽部（低濃度側槽
部）、３３・・・第２の濃縮槽部（高濃度側槽部）．FIG. 1 is a schematic diagram showing a concentrating facility according to one embodiment of the present invention, and FIG. 2 is a schematic diagram showing a concentrating facility according to another embodiment of the present invention. 1, 35... Concentration equipment, 2... First concentration tank (low accuracy side Mffl+), 3-. Second a! Li tank (high concentration 41+11 tank part), 4, 5... membrane module, 6.7
... Aeration pipe, 32... First concentration tank section (low concentration side tank section), 33... Second concentration tank section (high concentration side tank section).