JPH01231999A - Method for concentrating sludge - Google Patents
Method for concentrating sludgeInfo
- Publication number
- JPH01231999A JPH01231999A JP63057179A JP5717988A JPH01231999A JP H01231999 A JPH01231999 A JP H01231999A JP 63057179 A JP63057179 A JP 63057179A JP 5717988 A JP5717988 A JP 5717988A JP H01231999 A JPH01231999 A JP H01231999A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- concentration
- tank
- concn
- dilution
- 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
- 239000010802 sludge Substances 0.000 title claims abstract description 54
- 238000000034 method Methods 0.000 title claims description 12
- 238000010790 dilution Methods 0.000 claims abstract description 33
- 239000012895 dilution Substances 0.000 claims abstract description 33
- 230000005484 gravity Effects 0.000 claims abstract description 27
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims abstract description 19
- 238000007865 diluting Methods 0.000 claims abstract description 4
- 238000004094 preconcentration Methods 0.000 claims abstract description 4
- 239000012141 concentrate Substances 0.000 claims abstract description 3
- 230000008719 thickening Effects 0.000 claims description 5
- 238000012546 transfer Methods 0.000 claims description 4
- 230000007423 decrease Effects 0.000 abstract description 4
- 238000001514 detection method Methods 0.000 abstract 1
- 239000010865 sewage Substances 0.000 description 9
- 230000000694 effects Effects 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000007796 conventional method Methods 0.000 description 4
- 238000010586 diagram Methods 0.000 description 4
- 238000012545 processing Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 238000005273 aeration Methods 0.000 description 2
- 238000004140 cleaning Methods 0.000 description 2
- 239000010419 fine particle Substances 0.000 description 2
- 239000007788 liquid Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000000203 mixture Substances 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 238000000926 separation method Methods 0.000 description 2
- 239000006228 supernatant Substances 0.000 description 2
- 239000002351 wastewater Substances 0.000 description 2
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 239000000356 contaminant Substances 0.000 description 1
- 230000008602 contraction Effects 0.000 description 1
- 238000000354 decomposition reaction Methods 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- 238000011161 development Methods 0.000 description 1
- 239000006185 dispersion Substances 0.000 description 1
- 239000005446 dissolved organic matter Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 239000011499 joint compound Substances 0.000 description 1
- 239000005416 organic matter Substances 0.000 description 1
- 230000003647 oxidation Effects 0.000 description 1
- 238000007254 oxidation reaction Methods 0.000 description 1
- 238000005086 pumping Methods 0.000 description 1
- 239000002002 slurry Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000002699 waste material Substances 0.000 description 1
Landscapes
- Treatment Of Sludge (AREA)
Abstract
Description
【発明の詳細な説明】
（産業上の利用分野）
本発明は下水処理場等から発生する汚泥を効率良く濃縮
するために使用される汚泥のｔＭ縮方法の改良に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION (Field of Industrial Application) The present invention relates to an improvement in a sludge tM reduction method used for efficiently concentrating sludge generated from sewage treatment plants and the like.
（従来の技術）
下水処理場等における標準的な下水処理は、第５図に示
されるように初沈汚泥と最終沈澱池から返送されてきた
余剰汚泥との混合生汚泥をポンプにより引抜いて重力′
ａ縮槽へ送り込み重力濃縮させる方法によって行われて
いる。しかし近年においては下水中の有機＄Ｊ質が増加
し、汚泥表面に付着した有ｎ物質が重力濃縮を阻害する
ため、濃縮性の低下、沈降時間の増加、設備規模の大型
化、ｌチ泥の腐敗による汚泥浮上、脱水能力の低下や脱
水ケーキ水分の上昇等の種々の問題を生じている。(Prior art) As shown in Figure 5, standard sewage treatment at sewage treatment plants, etc. involves pumping out the raw sludge, which is a mixture of initial settling sludge and excess sludge returned from the final settling tank, using gravity. ′
This is carried out by feeding the water into a condensation tank and concentrating it by gravity. However, in recent years, organic substances in sewage have increased, and organic substances adhering to the sludge surface inhibit gravity concentration, resulting in decreased concentration, increased sedimentation time, larger equipment, and increased sludge. This has caused various problems such as sludge floating up due to decomposition, a decrease in dewatering capacity, and an increase in the moisture content of the dehydrated cake.
そこで最近では第６図に示されるように、混合生１η泥
を希釈槽へ導入して表面に付着している有機物質に由来
する粘着物を洗浄したうえで重力濃縮を行わ・ヒる希釈
洗浄法が開発され一部の下水処理場において実施されて
いる。ところが従来は一定倍率に希釈する方法が法用さ
れていたため、希釈槽へ流入する汚泥の濃度が低い場合
は過剰希釈となってその後の重力濃縮に却って時間がか
かることがあるうえ、希釈槽へ流入する汚泥のｌａ度が
変動するとそれにつれて重力濃縮槽へ流入する希釈され
た汚泥の濃度も変動し、受入負荷が不安定となって安定
した？Ｍｒ １Ｍ効果が得られないという問題があった
。Therefore, recently, as shown in Figure 6, the mixed raw 1η mud is introduced into a dilution tank, the sticky matter derived from organic substances adhering to the surface is washed, and then gravity concentration is carried out. A method has been developed and implemented in some sewage treatment plants. However, in the past, the method of diluting to a certain ratio was legally used, so if the concentration of sludge flowing into the dilution tank is low, it may become excessively diluted and the subsequent gravity concentration may take more time. When the la degree of the inflowing sludge changes, the concentration of the diluted sludge flowing into the gravity thickening tank also changes, and the receiving load becomes unstable and then becomes stable. There was a problem that the Mr 1M effect could not be obtained.
（発明が解決しようとする課題）
本発明は上記のような従来の問題点を解決して、有機物
の多いｌη泥を効率良く重カン３縮することができるう
え過剰希釈となることがなく、しかも混合生汚泥の濃度
が変動した場合にも安定した濃縮効果を得ることができ
る汚泥の濃縮方法を目的として完成されたものである。(Problems to be Solved by the Invention) The present invention solves the above-mentioned conventional problems, and can efficiently condense lη mud with a large amount of organic matter, without causing excessive dilution. Moreover, this method was completed with the aim of providing a sludge concentration method that can obtain a stable concentration effect even when the concentration of mixed raw sludge fluctuates.
（課題を解決するための手段）
上記の課題を達成するためになされた本発明は、最初沈
澱池より引抜いた混合生汚泥を希釈槽で希釈したうえ重
力濃縮する汚泥の濃縮方法において、混合化ｔη泥の濃
度を移送配管途中に設けた濃度計で検知し、濃度が設定
値以下に低下したときには引抜ポンプを停止させ、また
濃度が設定値を越えたときには併せて測定された流量と
の演算により希釈水ポンプを制御して１．５〜２．５倍
に希釈したのち予備濃縮して予（ｌＩｔ ｔ１４縮後の
７肩度を０．７〜１゜５％の範囲に維持しつつ重力濃縮
槽へ供給することを特徴とするものである。(Means for Solving the Problems) The present invention, which has been made to achieve the above-mentioned problems, is a sludge concentration method in which mixed raw sludge is first drawn out from a settling tank, diluted in a dilution tank, and then concentrated by gravity. The concentration of tη mud is detected with a concentration meter installed in the middle of the transfer pipe, and when the concentration drops below the set value, the withdrawal pump is stopped, and when the concentration exceeds the set value, calculation is performed with the measured flow rate. Control the dilution water pump to dilute 1.5 to 2.5 times, and then pre-concentrate it. It is characterized by being supplied to a concentration tank.
次に本発明を第１図のブロック図に従って更に詳細に説
明する。Next, the present invention will be explained in more detail with reference to the block diagram of FIG.
本発明においても汚水はまず沈砂池ｉｌ＋に導入され、
汚水中の粗大浮遊夾雑物や砂泥を除去したうえで最初沈
澱池（２）で砂泥や浮遊固形物質の沈降分離が行われる
。そしてその上澄水は曝気槽（３）において活性７１ｊ
泥法により生物処理され溶解性有機物の凝集、酸化を進
行させ、更に最終沈澱池（４）により上澄水とｌη泥と
に分月１される。この汚泥はポンプ（５）により最初沈
澱池（２）や曝気槽（３）へ返送される。また最初沈澱
池ｔｘｔから引抜かれた初沈ｌｌｊ泥と余剰汚泥との混
合物である混合生汚泥は、引抜ポンプ（６）により移送
配管（７）を介して希釈槽（８）へ移送され、ここで希
釈水槽（９）から赤釈水ポンプ００）により供給される
希釈水によって希釈され、ｌｒ３泥表面表面機物質が洗
浄される。Also in the present invention, wastewater is first introduced into the settling basin il+,
After removing coarse suspended contaminants and sand and mud from the wastewater, the sand and mud and suspended solids are first separated by sedimentation in a settling tank (2). Then, the supernatant water becomes active in the aeration tank (3).
The slurry is biologically treated by the mud method to promote flocculation and oxidation of dissolved organic matter, and is further divided into supernatant water and lη mud in the final settling tank (4). This sludge is first returned to the sedimentation tank (2) and aeration tank (3) by the pump (5). In addition, the mixed raw sludge, which is a mixture of the initially settled llj sludge and surplus sludge, which was drawn out from the first settling tank txt, is transferred to the dilution tank (8) via the transfer pipe (7) by the drawing pump (6), and is then transferred there. The lr3 mud surface is diluted with dilution water supplied from the dilution water tank (9) by the red water pump 00), and the lr3 mud surface material is washed.
上記の］二程は第６図に示された従来の７η泥希釈フロ
ーと特に変るところはないが、本発明においては移送配
管（７）の途中に流量計（１１）とｌＱ度計（１２）と
が設けられており、希釈槽（８）へ供給される混合生汚
泥の流量と濃度とを測定し、マイクロコンピュータのよ
うな演算器（１３）へ演算結果を入力している。この演
算器（１３）は引抜ポンプ（６）と希釈水ポンプＱｌｌ
とに接続してあり、もし移送される混合生汚泥の濃度が
設定値以下まで低下したときには引抜ポンプ（６）を停
止させる。設定値としては例えば０．５％を採用し、こ
れにより濃度が０．５％以下の汚泥が希釈槽（８）へ供
給されて過剰希釈されることが防止される。一方、混合
生汚泥の濃度がこの設定値を越えたときには希釈洗浄が
行われるのであるが、本発明においては従来のように一
定倍率で希釈するのではなく、流量計（１１）によって
測定された流量と濃度とを併せて演算したうえで、通常
ｌη泥濃度０．５〜２．０％の汚泥を希釈倍率が１．５
〜２．５倍の範囲内に維持されるように希釈水ポンプ（
Ｉｍを制御する。ここで希釈倍率として１．５〜２．５
倍を選択したのは希釈倍率が２．５倍以上となるとその
後の重力濃縮の効率が低下し、１．５倍を下まわると有
機物質の除去が十分に行われずやはり重力濃縮の効率が
低下するからである。なお、希釈、洗浄後の汚泥を予備
濃縮するのは、希釈、洗浄後の汚泥は沈降性が極めて良
好であり、通常２０〜３０分程度の滞留時間で簡単に０
．７〜１．５％に濃縮されるからである。なお濃度が０
．７％以下であると重力？Ｍ１ｉ？を槽（１５）の容屑
を極めて大型化しなければならなくなるので好ましくな
い。また１、５％以上であると重力’ｔＭ ４ｉ？ｉ槽
（１５）によるｌ麿縮性が悪くなる。このようにして希
釈倍率を１．５〜２．５倍となるように制御されつつ希
釈洗浄され打機物質を除去された希釈汚泥は予備濃縮槽
へ専かれ予備濃縮後の濃度を０６７〜１．５％としたの
ら、更に重力濃縮槽（１５）へ導かれ、１２〜２４時間
程度静置されて濃度が２〜４％となるまで重力濃縮が行
われる。このとき、希釈ｌη泥を予備分離槽（１４）内
に導いて２０〜３０分間にわたり微細粒子の越流除去を
行わ−Ｕたうえて重力濃縮槽（１５）へ導くようにすれ
ば、重力濃縮槽（１５）における静置時間を７０〜８０
％にまで減少させることができ、１・−タルの処理時間
を大幅に短縮することが可能となる。なお予６１η分乱
槽（１４）から生じた微細粒子を含む予備分離液は重力
濃縮槽から発生する分離液と同様に最初沈澱池（２）へ
戻される。The above steps] are not particularly different from the conventional 7η mud dilution flow shown in FIG. ) is provided to measure the flow rate and concentration of the mixed raw sludge supplied to the dilution tank (8), and input the calculation results to a calculation unit (13) such as a microcomputer. This computing unit (13) includes a drawing pump (6) and a dilution water pump Qll.
If the concentration of mixed raw sludge to be transferred falls below a set value, the drawing pump (6) is stopped. For example, 0.5% is adopted as the set value, thereby preventing sludge with a concentration of 0.5% or less from being supplied to the dilution tank (8) and being excessively diluted. On the other hand, when the concentration of mixed raw sludge exceeds this set value, dilution cleaning is performed, but in the present invention, instead of diluting at a fixed rate as in the past, After calculating the flow rate and concentration together, the dilution ratio of sludge with a normal lη mud concentration of 0.5 to 2.0% is 1.5.
Dilution water pump to maintain within ~2.5x range (
Control Im. Here, the dilution ratio is 1.5 to 2.5
The reason for choosing this ratio is that if the dilution ratio is 2.5 times or more, the efficiency of subsequent gravity concentration will decrease, and if it is less than 1.5 times, organic substances will not be removed sufficiently and the efficiency of gravity concentration will also decrease. Because it does. In addition, pre-concentrating the sludge after dilution and washing is because the sludge after dilution and washing has extremely good sedimentation properties, and can be easily concentrated in a residence time of about 20 to 30 minutes.
．． This is because it is concentrated to 7 to 1.5%. Note that the concentration is 0
．． Is it gravity if it is less than 7%? M1i? This is not preferable because the waste capacity of the tank (15) must be made extremely large. Also, if it is 1.5% or more, the gravity 'tM 4i? The shrinkability caused by the i-tank (15) deteriorates. In this way, the diluted sludge, which is diluted and washed while controlling the dilution ratio to be 1.5 to 2.5 times and from which the battering material has been removed, is sent to a pre-concentration tank where the concentration after pre-concentration is reduced to 0.67 to 1. Once the concentration is set at .5%, it is further led to a gravity concentration tank (15), and allowed to stand for about 12 to 24 hours, where gravity concentration is performed until the concentration reaches 2 to 4%. At this time, if the diluted lη mud is introduced into the preliminary separation tank (14) to remove overflow of fine particles for 20 to 30 minutes, and then introduced to the gravity concentration tank (15), gravity concentration The standing time in the tank (15) is 70 to 80 minutes.
%, making it possible to significantly shorten the processing time for 1.-tal. Note that the pre-separated liquid containing fine particles generated from the pre-61η dispersion tank (14) is returned to the initial settling tank (2) in the same way as the separated liquid generated from the gravity concentration tank.
以上に説明したように、本発明においては希釈後の濃度
が一定の範囲内の値となるように制御しつつ希釈洗浄を
行うので、その後の重力濃縮槽（１５）における到達ｌ
η泥濃度を従来法による場合よりも１〜１．５％も高め
ることができる。第２図のグラフは横軸に供給汚泥濃度
、縦軸に重力濃縮槽（１５）内に２４時間静置して重力
濃縮を行わせた場合の到達汚泥濃度を取って本発明の効
果を示したグラフであり、本発明によれば洗浄を行わな
い従来法に比較して重力Ｑ縮による到達汚泥濃度を最高
１゜５％以上も高めることができる。このように汚泥の
？ａ ′ｌｒ６？ｍ度を例えば従来の２％から３．３％
まで高めることができれば、第３図に示すように後工程
の脱水機の処理能力を３ ｋｇ ／ｍｚ−Ｈｒから４．
２ｋｇ／ｍ２・Ｈｒまで４０％も向上させることができ
、また第４図に示すように脱水ケーキの含水率を６７％
から６４．５％まで低下させることができる。この結果
、脱水ケーキの焼却処理に要する熱量を大幅に削減する
ことができ、下水処理場全体の処理能力の向上にも大き
く寄与することができる。As explained above, in the present invention, dilution cleaning is performed while controlling the concentration after dilution to be within a certain range, so that the concentration reached in the gravity concentration tank (15) after that is
The η mud concentration can be increased by 1 to 1.5% compared to the conventional method. The graph in Figure 2 shows the effects of the present invention, with the horizontal axis representing the supplied sludge concentration and the vertical axis representing the sludge concentration reached when the sludge is allowed to stand still in the gravity thickening tank (15) for 24 hours to carry out gravity thickening. The graph shows that according to the present invention, the achieved sludge concentration due to gravity Q contraction can be increased by at least 1.5% compared to the conventional method that does not perform washing. Of sludge like this? a′lr6? For example, increase m degree from 2% to 3.3%
If it is possible to increase the processing capacity of the dehydrator in the post-process from 3 kg/mz-Hr to 4.0 kg/mz-Hr, as shown in Figure 3.
The water content of the dehydrated cake can be increased by 40% to 2kg/m2・Hr, and the moisture content of the dehydrated cake can be increased to 67% as shown in Figure 4.
It can be reduced from 64.5% to 64.5%. As a result, the amount of heat required for incineration of the dehydrated cake can be significantly reduced, and this can greatly contribute to improving the treatment capacity of the entire sewage treatment plant.
（発明の効果）
本発明は以上の説明からも明らかなように、混合生汚泥
の濃度が設定値を下まわったときには引抜きを停止して
過剰希釈を防止することができ、また希釈後の汚泥の濃
度が所定の範囲内に維持されるように希釈水ポンプを制
御するので重力濃縮槽の受入負荷を安定させることがで
きる。そしてこれによって有機物質の含有゛ｒ４′−の
高いｌり水に対しても重力分離槽の到達汚泥濃度を向上
させることができることから、下水処理場の処理能力の
向上及び管理性の向上等の多くの実用的な効果を得るこ
とができる。よって本発明は従来の問題点を一掃した汚
泥の濃縮方法として、産業の発展に寄与するところは極
めて大である。(Effects of the Invention) As is clear from the above description, the present invention can stop drawing when the concentration of mixed raw sludge falls below a set value, preventing excessive dilution, and Since the dilution water pump is controlled so that the concentration of water is maintained within a predetermined range, the receiving load of the gravity thickening tank can be stabilized. As a result, it is possible to improve the sludge concentration achieved in the gravity separation tank even for sludge water with a high content of organic substances, so it is possible to improve the treatment capacity and manageability of sewage treatment plants. Many practical effects can be obtained. Therefore, the present invention greatly contributes to the development of industry as a method of concentrating sludge that eliminates the problems of the conventional method.
第１図は本発明の下水処理フローを示すブロック図、第
２図は本発明と従来法とによる到達ｌη泥ｌ；度を示づ
グラフ、第３図は汚泥濃度と脱水機の処理能力との関係
を示すグラフ、第４図は汚泥濃度と脱水ケーキの含水率
との関係を示すグラフ、第５図は下水処理の標準フロー
を示すブロック図、第６図は従来の汚泥希釈フローを示
すブロック図である。
（２）：最初沈澱池、（７）：移送配管、（８）：希釈
槽、００１：希釈水ポンプ、（１１）：流■計、（１２
） ：濃度計、（１５） ：重力濃縮槽。Fig. 1 is a block diagram showing the sewage treatment flow of the present invention, Fig. 2 is a graph showing the sludge concentration achieved by the present invention and the conventional method, and Fig. 3 is a graph showing the sludge concentration and the processing capacity of the dehydrator. Figure 4 is a graph showing the relationship between sludge concentration and water content of dehydrated cake, Figure 5 is a block diagram showing the standard flow of sewage treatment, and Figure 6 shows the conventional sludge dilution flow. It is a block diagram. (2): First sedimentation tank, (7): Transfer piping, (8): Dilution tank, 001: Dilution water pump, (11): Flowmeter, (12
): Concentration meter, (15): Gravity concentration tank.
Claims (1)
うえ重力濃縮する汚泥の濃縮方法において、混合生汚泥
の濃度を移送配管途中に設けた濃度計で検知し、濃度が
設定値以下に低下したときには引抜ポンプを停止させ、
また濃度が設定値を越えたときには併せて測定された流
量との演算により希釈水ポンプを制御して１．５〜２．
５倍に希釈したのち予備濃縮して予備濃縮後の濃度を０
．７〜１．５％の範囲に維持しつつ重力濃縮槽へ供給す
ることを特徴とする汚泥の濃縮方法。In a sludge concentration method in which mixed raw sludge is first pulled out from a settling tank, diluted in a dilution tank, and then concentrated by gravity, the concentration of mixed raw sludge is detected by a concentration meter installed in the transfer pipe, and the concentration drops below the set value. When this happens, stop the withdrawal pump,
In addition, when the concentration exceeds the set value, the dilution water pump is controlled by calculation with the measured flow rate at 1.5 to 2.
After diluting 5 times, pre-concentrate the concentration after pre-concentration to 0.
．． A method for concentrating sludge, which comprises supplying sludge to a gravity thickening tank while maintaining the concentration within a range of 7 to 1.5%.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63057179A JPH0732919B2 (en) | 1988-03-10 | 1988-03-10 | Sludge concentration method |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP63057179A JPH0732919B2 (en) | 1988-03-10 | 1988-03-10 | Sludge concentration method |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH01231999A true JPH01231999A (en) | 1989-09-18 |
| JPH0732919B2 JPH0732919B2 (en) | 1995-04-12 |
Family
ID=13048293
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP63057179A Expired - Lifetime JPH0732919B2 (en) | 1988-03-10 | 1988-03-10 | Sludge concentration method |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0732919B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5462672A (en) * | 1992-08-13 | 1995-10-31 | Chemical Grouting Co., Ltd. | Process for treating sludge and system for the same |
| JP2012096210A (en) * | 2010-11-05 | 2012-05-24 | Swing Corp | Treatment method and treatment apparatus of organic sludge |
| JP2013144298A (en) * | 2013-05-01 | 2013-07-25 | Swing Corp | Method and device for treating organic sludge |
-
1988
- 1988-03-10 JP JP63057179A patent/JPH0732919B2/en not_active Expired - Lifetime
Cited By (4)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US5462672A (en) * | 1992-08-13 | 1995-10-31 | Chemical Grouting Co., Ltd. | Process for treating sludge and system for the same |
| US5624550A (en) * | 1992-08-13 | 1997-04-29 | Chemical Grouting Co., Ltd. | Process for treating sludge and system for the same |
| JP2012096210A (en) * | 2010-11-05 | 2012-05-24 | Swing Corp | Treatment method and treatment apparatus of organic sludge |
| JP2013144298A (en) * | 2013-05-01 | 2013-07-25 | Swing Corp | Method and device for treating organic sludge |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0732919B2 (en) | 1995-04-12 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US5068031A (en) | Sludge treatment apparatus | |
| JPH0338300A (en) | Concentration and dehydration of slurry-like sludge | |
| JPH08257583A (en) | Waste water treatment apparatus | |
| CN106458669B (en) | Method for clarifying waste water | |
| JPH01231999A (en) | Method for concentrating sludge | |
| JP4118191B2 (en) | Coagulation sedimentation processing equipment | |
| JPH10314505A (en) | Method for treating organic wastewater | |
| JP2001170656A (en) | Process for removing solid particulate, more particularly silica and/or alumina particulate from waste water | |
| Wang et al. | Flotation thickening | |
| JP2001017982A (en) | Method and device for treating waste water | |
| JPH09290273A (en) | Method for adjusting amount of flocculant to be added and device therefor | |
| NL8902609A (en) | METHOD FOR SEPARATING A SOLID PHASE FROM A LIQUID, IN PARTICULAR FOR THE PURIFICATION OF WASTE WATER. | |
| JP3973967B2 (en) | Coagulation separation device | |
| JP3835610B2 (en) | Wastewater treatment method and apparatus | |
| JPH02277597A (en) | Treatment of organic sewage | |
| CN219709319U (en) | Fluorine-containing wastewater treatment system | |
| JPH0377700A (en) | Method for thickening sludge | |
| CN113480033A (en) | Sewage treatment device and method for industrial circulating cooling water system | |
| JP2018079402A (en) | Sewage treatment system and sewage treatment method | |
| JP2003326110A (en) | Flocculation and separation apparatus | |
| JPS58214395A (en) | Treatment of waste water | |
| JPS58183914A (en) | Apparatus for controlling waste sludge of concentration tank | |
| JPS6099400A (en) | Sludge concentrator | |
| JPS6311077B2 (en) | ||
| JP2001259682A (en) | Waste water treating apparatus |