JP2003175400A - Method for treatment of sewage sludge - Google Patents
Method for treatment of sewage sludgeInfo
- Publication number
- JP2003175400A JP2003175400A JP2001379572A JP2001379572A JP2003175400A JP 2003175400 A JP2003175400 A JP 2003175400A JP 2001379572 A JP2001379572 A JP 2001379572A JP 2001379572 A JP2001379572 A JP 2001379572A JP 2003175400 A JP2003175400 A JP 2003175400A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- concentrated
- treatment
- dehydrator
- sewage
- 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
Landscapes
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、下水汚泥等の脱水
前の前処理において、汚泥の一部を濃縮処理することに
より脱水性を向上させ、活性余剰汚泥の前処理手段とし
て利用できるようにした下水汚泥の処理方法に関するも
のである。TECHNICAL FIELD The present invention relates to a pretreatment of sewage sludge or the like before dehydration so that a part of the sludge is concentrated to improve the dehydration property and can be used as a pretreatment means for activated surplus sludge. The present invention relates to a method for treating sewage sludge.
【０００２】[0002]
【従来の技術】従来、下水処理場より発生する活性余剰
汚泥あるいは活性余剰汚泥と初沈汚泥との混合生汚泥に
凝集剤を添加し、脱水処理する場合、汚泥濃度が低いと
大型の脱水機が必要となったり、脱水機の種類によって
は脱水処理することが困難であったりすることから、汚
泥を凝集濃縮した後に脱水処理することは特開平７−３
１９９９号公報や特開平８−３２３３９９号公報に記載
してあるように公知である。2. Description of the Related Art Conventionally, when a flocculant is added to an activated surplus sludge generated from a sewage treatment plant or a mixed raw sludge containing an activated surplus sludge and a first settling sludge for dehydration treatment, a large-sized dehydrator with a low sludge concentration is used. However, it is difficult to perform the dehydration treatment depending on the type of dehydrator. Therefore, it is not possible to perform the dehydration treatment after coagulating and concentrating sludge.
It is publicly known as described in 1999 and Japanese Patent Laid-Open No. 8-323399.
【０００３】[0003]
【発明が解決しょうとする課題】上述の特開平７−３１
９９９号公報に記載してある汚泥処理方法は、有機汚泥
にアニオン性高分子凝集剤を添加撹拌後、この汚泥にカ
チオン性高分子凝集剤を添加撹拌し、凝集フロックを生
成させ、この凝集汚泥に高分子凝集剤分散液を添加して
濃縮装置で予備濃縮を行なうか、あるいはこの凝集汚泥
を濃縮装置で予備濃縮した後、スクリュープレス前段の
ホッパーに高分子凝集剤分散液を水と混合しながら、こ
の凝集汚泥に添加して脱水処理を行なう汚泥の処理方法
である。そして、特開平８−３２３３９９号公報に記載
の汚泥処理方法は、凝集剤を添加する前段において汚泥
の全量を膜濃縮装置で分離液と濃縮汚泥に分離し、この
濃縮汚泥に高分子凝集剤を添加して撹拌凝集後、この凝
集汚泥に分離液の一部を添加混合することにより、分離
液中に残存しているアニオン分を利用してさらに凝集を
促進させ、この汚泥を脱水機で脱水処理を行なうように
した汚泥の処理方法である。DISCLOSURE OF THE INVENTION Problems to be Solved by the Invention
In the sludge treatment method described in Japanese Patent Publication No. 999, an anionic polymer coagulant is added to an organic sludge and stirred, and then a cationic polymer coagulant is added to this sludge and stirred to generate coagulated flocs. Polymer flocculant dispersion is added to and pre-concentrated with a concentrator, or this flocculated sludge is pre-concentrated with a concentrator, and then the polymer flocculant dispersion is mixed with water in the hopper before the screw press. However, this is a sludge treatment method in which dehydration treatment is performed by adding to the coagulated sludge. Then, in the sludge treatment method described in JP-A-8-323399, the total amount of sludge is separated into a separation liquid and a concentrated sludge by a membrane concentrator in the previous stage of adding the coagulant, and the concentrated coagulant contains a polymer coagulant. After adding and stirring to agglomerate, a part of the separated liquid is added and mixed to this agglomerated sludge to further promote the agglomeration by utilizing the anion component remaining in the separated liquid, and the sludge is dehydrated with a dehydrator. This is a sludge treatment method adapted to perform treatment.
【０００４】しかしながら、特開平７−３１９９９号公
報に記載の発明においては、アニオン及びカチオンの２
種類の高分子凝集剤を使用するため、１種類の高分子凝
集剤で汚泥処理を行なう方法に比べ、薬注設備が余分に
必要で、設置スペースも広くなり、ランニングコストも
嵩むという課題がある。さらに、スクリーン濃縮機によ
って最大に濃縮をおこなうため、濃縮汚泥の流動性が低
くなる恐れが有り、流動性の低い汚泥をスクリュープレ
スに圧入すれば、スクリューの回転に非常に大きいトル
クが必要となり、外筒のろ材にかかる負荷も非常に大き
くなるので、スクリュープレスの強度や所要動力が大き
くなるため、設備費用が嵩むという課題もある。また、
特開平８−３２３３９９号公報に記載の発明において
は、濃縮装置に膜を使用しているため、濃縮装置自体が
高価であり、膜の維持管理に要する費用も高くつくもの
である。そして、濃縮汚泥に膜の分離液を添加して、分
離液中のアニオン分によって凝集を促進するようにした
ものであるが、膜の分離液中には汚泥粒子の存在が非常
に少ないため、汚泥粒子の表面のアニオン基も少なく、
凝集を促進するためのアニオン量の調節が難しいという
課題が有る。However, in the invention described in Japanese Patent Laid-Open No. 7-31999, there are two anions and two cations.
Since different types of polymer flocculants are used, compared to the method of treating sludge with one type of polymer flocculant, extra chemical dosing equipment is required, the installation space is wide, and running costs are high. . Furthermore, since the screen concentrator performs maximum concentration, there is a risk that the fluidity of the concentrated sludge will be low.If sludge with low fluidity is pressed into the screw press, a very large torque is required to rotate the screw, Since the load applied to the filter material of the outer cylinder also becomes very large, the strength and required power of the screw press become large, which causes a problem that the equipment cost increases. Also,
In the invention described in JP-A-8-323399, since the membrane is used in the concentrating device, the concentrating device itself is expensive, and the cost required for the maintenance of the membrane is high. Then, the separation liquid of the membrane is added to the concentrated sludge so as to promote coagulation by the anion component in the separation liquid, but since the presence of sludge particles in the separation liquid of the membrane is very small, There are few anion groups on the surface of sludge particles,
There is a problem that it is difficult to control the amount of anions for promoting aggregation.
【０００５】[0005]
【課題を解決するための手段】前述した課題を解決する
ため、本発明は下水汚泥の一部にカチオン系高分子凝集
剤を添加して撹拌機で混合撹拌を行ない、凝集フロック
を生成させる。そして、この凝集汚泥を回転式の濃縮機
で濃縮した後、この濃縮汚泥に残りの原汚泥を供給し、
さらに、少量のカチオン系高分子凝集剤を添加して撹拌
機で混合撹拌することにより、凝集性を復元することが
でき、脱水性が向上するようにした下水汚泥の処理方法
である。そして、上記下水汚泥の処理方法において、濃
縮機で濃縮操作を行なう汚泥は原汚泥量の５０〜８０％
とし、濃縮倍率は５〜１５倍となるようにしたものであ
る。また、上記の濃縮汚泥の固液分離を行なう脱水機と
して圧入式スクリュープレスや連続式加圧型脱水機等の
圧入型脱水機を使用することにより、効率の良い脱水処
理を行なうことができるものである。In order to solve the above-mentioned problems, the present invention adds a cationic polymer flocculant to a part of sewage sludge and mixes and stirs with a stirrer to generate floc. Then, after concentrating this coagulated sludge with a rotary concentrator, the remaining original sludge is supplied to this concentrated sludge,
Furthermore, it is a method for treating sewage sludge in which a small amount of a cationic polymer flocculant is added and mixed and stirred by a stirrer so that cohesiveness can be restored and dehydration can be improved. And in the method of treating sewage sludge, the sludge to be concentrated by the concentrator is 50 to 80% of the original sludge amount.
The concentration ratio is 5 to 15 times. Further, by using a press-fitting type dehydrator such as a press-fitting type screw press or a continuous pressurizing type dehydrator as a dehydrator for performing solid-liquid separation of the concentrated sludge, it is possible to perform an efficient dehydration treatment. is there.
【０００６】[0006]
【発明の実施の形態】本発明に係る実施の形態を以下に
説明するが、本発明がこれに限定されるものでないこと
は勿論のことである。下水処理場で発生する活性余剰汚
泥あるいは活性余剰汚泥と初沈汚泥との混合生汚泥は汚
泥濃度が低く、高分子凝集剤を添加して凝集させたフロ
ックの強度も弱い。そのため、この凝集汚泥を直接脱水
機で処理すると処理能力が低く、脱水したケーキ水分も
高く、大規模な脱水機が必要となる。また、脱水前に凝
集汚泥を全量濃縮して脱水処理を行なう場合においても
高分子凝集剤を添加して凝集させた汚泥を濃縮機で濃縮
した時点で凝集フロックの破壊が起り、処理能力やケー
キ水分が期待した通りの効果が出ない。そして、濃縮汚
泥を脱水前に再度高分子凝集剤を添加して再凝集させる
場合でも、凝集効率が悪く、薬品代が高くつく。BEST MODE FOR CARRYING OUT THE INVENTION Embodiments of the present invention will be described below, but it goes without saying that the present invention is not limited thereto. Activated surplus sludge generated from sewage treatment plants or mixed raw sludge of activated surplus sludge and primary sedimentation sludge has a low sludge concentration, and the strength of flocs coagulated by adding a polymer coagulant is also weak. Therefore, if this coagulated sludge is directly treated with a dehydrator, the treatment capacity is low, the moisture content of the dehydrated cake is high, and a large-scale dehydrator is required. In addition, even in the case where the whole sludge is concentrated and dehydrated before dehydration, the floc of flocs occurs when the sludge aggregated by adding the polymer flocculant is concentrated by the concentrator, resulting in the treatment capacity and cake. Moisture does not work as expected. Even when the concentrated sludge is re-aggregated by adding a polymer coagulant before dehydration, the coagulation efficiency is poor and the cost of chemicals is high.
【０００７】本発明では、上記汚泥を効率良く脱水処理
を行なうための前処理方法において使用される。以下、
図１のフローシートに基づき本発明の処理方法を説明す
る。図１に示すように、下水処理場で発生する活性余剰
汚泥あるいは混合生汚泥の低濃度の下水汚泥Ａが汚泥貯
留槽１に供給される。符号１ａは汚泥の沈降防止のため
に設けた撹拌機である。この汚泥貯留槽１に貯留された
下水汚泥Ａの５０〜８０％の量を汚泥移送ポンプ２ａで
濃縮機３に供給する。この時、汚泥移送ポンプ２ａと濃
縮機３との間の汚泥供給ラインに高分子凝集剤貯留槽４
に貯留している高分子凝集剤を定量式の高分子凝集剤供
給ポンプ５ａによって一定量だけ汚泥に添加する。使用
する高分子凝集剤は下水汚泥の場合にはカチオン性高分
子凝集剤が有効で効果的である。高分子凝集剤を添加さ
れた下水汚泥中の懸濁物質はアニオン基の電位が中和さ
れ、懸濁物質同志が凝集してフロック化が促進する。そ
して、この凝集汚泥は濃縮機３のスクリーン３ａを駆動
機３ｂで回転させながら濃縮操作を行ない、５〜１５倍
に濃縮された汚泥は濃縮機３の汚泥排出口３ｃから自然
流下で汚泥混合槽６に投入される。濃縮機３で分離され
た分離液は機外に排出される。この時の濃縮汚泥量は１
／５〜１／１５に減少する。In the present invention, the sludge is used in a pretreatment method for efficiently dehydrating the sludge. Less than,
The processing method of the present invention will be described based on the flow sheet of FIG. As shown in FIG. 1, a low concentration sewage sludge A of activated surplus sludge or mixed raw sludge generated in a sewage treatment plant is supplied to a sludge storage tank 1. Reference numeral 1a is a stirrer provided to prevent sludge from settling. The sludge transfer pump 2a supplies 50% to 80% of the sewage sludge A stored in the sludge storage tank 1 to the concentrator 3. At this time, the polymer coagulant storage tank 4 is installed in the sludge supply line between the sludge transfer pump 2a and the concentrator 3.
A fixed amount of the polymer flocculant stored in the sludge is added to the sludge by the quantitative polymer flocculant supply pump 5a. As the polymer coagulant to be used, a cationic polymer coagulant is effective and effective in the case of sewage sludge. The suspended substance in the sewage sludge to which the polymer flocculant is added neutralizes the potential of the anion group, and the suspended substances coagulate to promote flocculation. Then, this agglomerated sludge is concentrated while rotating the screen 3a of the concentrator 3 with the driving device 3b, and the sludge concentrated 5 to 15 times is sludge mixing tank under natural flow from the sludge discharge port 3c of the concentrator 3. It is thrown into 6. The separated liquid separated by the concentrator 3 is discharged to the outside of the machine. The amount of concentrated sludge at this time is 1
It decreases to / 5 to 1/15.
【０００８】上述の汚泥混合槽６に汚泥貯留槽１に残っ
ている未濃縮汚泥を汚泥移送ポンプ２ｂで供給し、撹拌
機６ａで濃縮汚泥と未濃縮汚泥とを混合することによ
り、凝集性が復元するものである。そして、この混合汚
泥を一軸ネジポンプ等の定量式の汚泥供給ポンプ７で密
閉型の凝集混和槽８へ圧送するとともに、定量式の高分
子凝集剤供給ポンプ５ｂで高分子凝集剤を少量、凝集混
和槽８に供給し、撹拌機８ａで混合汚泥と高分子凝集剤
とを混合撹拌することにより、汚泥中の固形物を再凝集
させ、強固なフロックを生成するとともに、この凝集汚
泥を脱水機９（図１ではスクリュープレス９ａとしてい
る）への圧入圧力を一定になるように、圧力制御器（Ｐ
ＩＣ）８ｂで汚泥供給ポンプ７の汚泥供給量を制御しな
がらスクリュープレス９ａの軸芯より圧入する。The unconcentrated sludge remaining in the sludge storage tank 1 is supplied to the above sludge mixing tank 6 by the sludge transfer pump 2b, and the agitator 6a mixes the concentrated sludge and the unconcentrated sludge so that cohesiveness is improved. It is to be restored. Then, this mixed sludge is pressure-fed to a closed type coagulation and mixing tank 8 by a quantitative sludge supply pump 7 such as a single screw pump, and a small amount of the macromolecular coagulant is coagulated and mixed by a quantitative polymer coagulant supply pump 5b. The sludge is supplied to the tank 8, and the mixed sludge and the polymer flocculant are mixed and stirred by the stirrer 8a to re-aggregate the solid matter in the sludge to generate strong flocs, and the condensed sludge is dewatered by the dehydrator 9 In order to keep the press-fitting pressure to the screw press (9a in FIG. 1) constant, a pressure controller (P
IC) 8b, while controlling the sludge supply amount of the sludge supply pump 7, the sludge supply pump 7 is press-fitted from the shaft center of the screw press 9a.
【０００９】次に、図２に基づき上記の凝集汚泥の脱水
処理について説明するが、その前に、圧入式脱水機のス
クリュープレス９ａについて詳述する。スクリュープレ
ス９ａは、ろ室を形成する外筒スクリーン９ｄとスクリ
ュー軸９ｅ、ろ室内の汚泥に脱水力を与えるスクリュー
軸９ｅと一体になったスクリュー羽根９ｆ、スクリュー
軸９ｅを回転させる駆動機９ｇ、脱水ケーキ水分を調整
するプレッサー装置９ｈ等で構成されている。以下に各
部の構造を詳述する。Next, the dehydration treatment of the above coagulated sludge will be described with reference to FIG. 2, but before that, the screw press 9a of the press-fitting type dehydrator will be described in detail. The screw press 9a includes an outer cylinder screen 9d that forms a filter chamber, a screw shaft 9e, screw blades 9f that are integrated with the screw shaft 9e that applies a dehydrating force to sludge in the filter chamber, a drive unit 9g that rotates the screw shaft 9e, It is composed of a presser device 9h for adjusting the water content of the dehydrated cake. The structure of each part will be described in detail below.
【００１０】外筒スクリーン９ｄはスクリーンを支持す
る外筒と１．５ｍｍφ〜０．５ｍｍφ孔のパンチングプ
レートを使用したろ材で構成され、パンチングプレート
の孔は汚泥投入側が大きく、脱水ケーキ排出側に向かっ
て小さな孔で形成されている。スクリュー軸９ｅはその
外周部にスパイラル状のスクリュー羽根９ｆを固着した
ものである。このスクリュー軸９ｅは、汚泥投入側から
脱水ケーキ排出側に向かって太くなっている円錐形状を
しており、外筒スクリーン９ｄとスクリュー軸９ｅで形
成されるろ室は、脱水ケーキ排出側に向かってその容積
を連続的に小さくしている。そして、プレッサー装置９
ｈは、脱水ケーキ排出部に設けたテーパーコーン型の押
圧板で、エアーシリンダーで前後に移動するようになっ
ており、排出される脱水ケーキの含水率をある一定に保
てるようになっている。The outer cylinder screen 9d is composed of an outer cylinder for supporting the screen and a filter medium using a punching plate having holes of 1.5 mmφ to 0.5 mmφ. The hole of the punching plate has a large sludge charging side and a draining cake discharging side. Are formed with small holes. The screw shaft 9e has a spiral screw blade 9f fixed to the outer periphery thereof. The screw shaft 9e has a conical shape that is thicker from the sludge input side toward the dehydrated cake discharge side, and the filter chamber formed by the outer cylinder screen 9d and the screw shaft 9e faces the dehydrated cake discharge side. The volume is continuously reduced. And the presser device 9
Reference numeral h is a taper cone type pressing plate provided in the dehydrated cake discharging part, which is moved forward and backward by an air cylinder, so that the water content of the discharged dehydrated cake can be kept constant.
【００１１】上記のように構成したスクリュープレス９
ａの軸芯より圧入された凝集汚泥は供給孔９ｃから濃縮
ゾーンＢへ圧入され、ここで圧入圧力による濃縮が行な
われ、続いてスクリュー羽根９ｆによってろ過ゾーンＣ
へと搬送され、さらに、圧搾ゾーンＤへと送られる。上
述したようにろ室は汚泥投入側からケーキ排出側に向か
って容積が小さくなっているため、汚泥はこの容積変化
とスクリュー羽根９ｆによるスラスト力を受け、内部圧
力を次第に上昇させながら圧搾脱水され、ろ液とケーキ
に分離され、ケーキ排出側まできた脱水ケーキは、プレ
ッサー装置９ｈの押圧を押しのけて機外に排出されるも
のである。以上は本発明の下水汚泥の処理方法におい
て、スクリュープレス９ａを用いて脱水処理を行なう場
合について説明したものであるが、回転加圧脱水機９ｂ
等の圧入型脱水機を用いても同様の効果が奏せられる。The screw press 9 constructed as described above
The coagulated sludge press-fitted from the shaft core of a is press-fitted into the concentration zone B from the supply hole 9c, where it is concentrated by the press-fitting pressure, and then the screw blade 9f is used to perform the filtration zone C.
To the pressing zone D. As described above, since the volume of the filter chamber decreases from the sludge input side toward the cake discharge side, the sludge receives the volume change and the thrust force by the screw blades 9f, and is squeezed and dehydrated while gradually increasing the internal pressure. The dehydrated cake that has been separated into the filtrate and the cake and has reached the cake discharge side is discharged to the outside of the machine by pushing away the pressure of the presser device 9h. The above is a description of the case of performing the dehydration treatment using the screw press 9a in the method for treating sewage sludge of the present invention.
The same effect can be obtained by using a press-fitting type dehydrator such as.
【００１２】[0012]
【実施例】以下に、本発明の汚泥処理方法で脱水効率が
向上する効果を確かめるために行なった脱水試験を説明
する。
試験機仕様
濃縮試験を行なった濃縮機の仕様は次の通りである。
・型式 円筒スクリーン回転式濃縮機
・スクリーン径 ３００φ（ｍｍ）
・スクリーン長さ ４５０Ｌ（ｍｍ）
・スクリーン孔径 １．０φ（ｍｍ）
・有効ろ過面積 ０．４４ｍ2
・回転数 １．５〜３３ｒｐｍ
脱水試験を行なった脱水機の仕様は次の通りである。
・型式 スクリュープレス型脱水機
・スクリーン径 ２００φ（ｍｍ）
・スクリーン長さ １０００Ｌ（ｍｍ）
・スクリーン孔径 ０．５〜１．５φ（ｍｍ）EXAMPLE A dehydration test conducted to confirm the effect of improving the dehydration efficiency by the sludge treatment method of the present invention will be described below. Tester specifications The specifications of the concentrator used for the concentration test are as follows.・ Model Cylindrical screen rotary concentrator ・ Screen diameter 300φ (mm) ・ Screen length 450L (mm) ・ Screen pore diameter 1.0φ (mm) ・ Effective filtration area 0.44m 2・ Rotation speed 1.5-33rpm Dehydration test The specifications of the dehydrator that carried out are as follows.・ Model Screw press type dehydrator ・ Screen diameter 200φ (mm) ・ Screen length 1000L (mm) ・ Screen hole diameter 0.5 ~ 1.5φ (mm)
【００１３】脱水試験結果を以下に示す。
試験日 平成１３年７月〜１１月
試験場所 某下水処理場内
試験原液 混合生汚泥Ａ（汚泥濃度０．５％Ｗ／Ｖ）
混合生汚泥Ｂ（汚泥濃度１．０％Ｗ／Ｖ）
余剰汚泥（汚泥濃度０．４％Ｗ／Ｖ）
使用高分子 カチオン系高分子凝集剤
以下、表１・表２・表３に各試験原液の脱水試験結果を
示す。The results of the dehydration test are shown below. Test date July-November 2001 Test place Test stock solution in a certain sewage treatment plant Mixed raw sludge A (sludge concentration 0.5% W / V) Mixed raw sludge B (sludge concentration 1.0% W / V) Excess sludge (Sludge concentration 0.4% W / V) Polymer used Cationic polymer flocculant The results of the dehydration test of each test stock solution are shown below in Tables 1, 2 and 3.
【００１４】[0014]
【表１】 [Table 1]
【００１５】[0015]
【表２】 [Table 2]
【００１６】[0016]
【表３】 [Table 3]
【００１７】表１・表２・表３より原汚泥を濃縮操作を
行なわないで脱水した場合と、全量濃縮を行なって脱水
した場合とを比較すると、混合生汚泥Ａ、混合生汚泥
Ｂ、余剰汚泥ともにケーキ含水率は低下し、ろ過速度は
大幅に向上している。そして、高分子凝集剤の使用量も
減少している。尚、原汚泥を濃縮操作を行なわないで脱
水する場合のスクリュープレス９ａの回転数を０．５ｒ
ｐｍとしたのは、ケーキ含水率が高くなり過ぎ、目標値
（脱水後のケーキ処分に要する費用等から算出した数
値）を達成することが出来ないためである。混合生汚泥
Ａ及び混合生汚泥Ｂのケーキ含水率の目標値は７７％に
設定し、余剰汚泥のケーキ含水率の目標値は８７％に設
定した。From Table 1, Table 2 and Table 3, comparing the case where the raw sludge was dehydrated without performing the concentration operation and the case where the total sludge was concentrated and dehydrated were compared, mixed raw sludge A, mixed raw sludge B and surplus The water content of the cake in both the sludge and the filtration rate is significantly improved. Also, the amount of the polymer flocculant used is decreasing. When the raw sludge is dehydrated without performing the concentration operation, the rotation speed of the screw press 9a is 0.5r.
The reason for setting pm is that the water content of the cake becomes too high and the target value (a value calculated from the cost required for disposal of the cake after dehydration or the like) cannot be achieved. The target value of the cake water content of the mixed raw sludge A and the mixed raw sludge B was set to 77%, and the target value of the cake water content of the excess sludge was set to 87%.
【００１８】次に、全量濃縮汚泥と濃縮汚泥に原汚泥を
混合した汚泥とを比較してみると、まず、表１の混合生
汚泥Ａについては濃縮汚泥：原汚泥の混合比が２：１及
び１：１の濃縮汚泥＋原汚泥では高分子凝集剤の使用
量、ケーキ含水率、ろ過速度ともに向上しており、良好
な結果が得られている。又、濃縮汚泥：原汚泥の混合比
が１：２の場合はケーキ含水率が若干高くなっている点
を除けば、高分子凝集剤の使用量、ろ過速度の向上がみ
られる。表２の混合生汚泥Ｂにおいては濃縮汚泥：原汚
泥の全ての混合比で高分子凝集剤の使用量、ろ過速度の
向上がみられた。ケーキ含水率については、混合比１：
１のものが向上している以外は、全量濃縮汚泥のほうが
良好となっている。しかし、全ての混合比においてケー
キ含水率の目標値は達成している。表３の余剰汚泥につ
いては混合比１：３の汚泥が高分子凝集剤の使用量、ろ
過速度、ケーキ含水率の全てにおいて良好となってい
る。又、高分子凝集剤の使用量においても全ての混合比
で同じかあるいは向上している。ケーキ含水率について
は混合比が１：３より大きくなるほど高くなる傾向とな
っている。ろ過速度も混合比が１：３をピークとして混
合比が大きくなるほど、ろ過速度は低下している。Next, comparing the total sludge and the sludge obtained by mixing the original sludge with the concentrated sludge, first, for the mixed raw sludge A in Table 1, the mixing ratio of concentrated sludge to original sludge is 2: 1. In the 1: 1 concentrated sludge + raw sludge, the amount of the polymer flocculant used, the water content of the cake, and the filtration rate were improved, and good results were obtained. Further, when the mixing ratio of concentrated sludge to raw sludge is 1: 2, the amount of polymer flocculant used and the filtration rate are improved except that the cake water content is slightly higher. In the mixed raw sludge B in Table 2, the use amount of the polymer flocculant and the filtration rate were improved at all mixing ratios of concentrated sludge: original sludge. Regarding the water content of the cake, the mixing ratio is 1:
All of the concentrated sludges are better, except for No. 1. However, the target value of cake water content was achieved at all mixing ratios. Regarding the excess sludge in Table 3, the sludge with a mixing ratio of 1: 3 is good in all of the usage amount of the polymer flocculant, the filtration rate, and the cake water content. Also, the amount of the polymer flocculant used is the same or improved at all mixing ratios. The cake water content tends to increase as the mixing ratio becomes larger than 1: 3. As for the filtration rate, the mixing rate becomes a peak at a mixing ratio of 1: 3, and the filtering rate decreases as the mixing ratio increases.
【００１９】上記、脱水試験結果を考察すると、混合生
汚泥Ａにおいては濃縮汚泥：原汚泥の混合比が２：１の
場合が良好な結果を示している。次に、混合生汚泥Ｂに
おいては混合比が１：１の場合が最も良好な結果を示し
ている。そして、余剰汚泥については混合比が１：３の
場合が最も良好な結果となっている。Considering the above dehydration test results, in the mixed raw sludge A, good results are shown when the mixing ratio of concentrated sludge: original sludge is 2: 1. Next, in the mixed raw sludge B, the best result is shown when the mixing ratio is 1: 1. For the excess sludge, the best result is obtained when the mixing ratio is 1: 3.
【００２０】[0020]
【発明の効果】上述実施例のように、下水汚泥の一部に
高分子凝集剤を添加して混合撹拌を行ない凝集フロック
を生成させる。次に、この凝集汚泥を濃縮機で濃縮処理
を行ない、この濃縮汚泥に未濃縮の原汚泥を供給して少
量の高分子凝集剤を添加後、混合撹拌することにより、
凝集性が復元して脱水性が向上するものであり、使用す
る高分子凝集剤が減量でき、脱水ケーキ水分の低下、ろ
過速度の向上が図れ、効率の良い脱水処理を行なうこと
ができる下水汚泥の処理方法である。As in the above-mentioned embodiment, a polymer flocculant is added to a part of the sewage sludge and mixed and stirred to generate floc. Next, the coagulation sludge is concentrated by a concentrator, and an unconcentrated raw sludge is supplied to the concentrated sludge to add a small amount of a polymer coagulant, followed by mixing and stirring.
This is a sewage sludge that restores cohesiveness and improves dewatering ability, can reduce the amount of polymer flocculant used, reduce the water content of the dehydrated cake, improve the filtration rate, and perform efficient dewatering treatment. Is the processing method of.
【図１】本発明に係る下水汚泥の処理方法のフローシー
ト図である。FIG. 1 is a flow sheet diagram of a method for treating sewage sludge according to the present invention.
【図２】本発明に係る下水汚泥の処理方法で使用する脱
水機の概念図である。FIG. 2 is a conceptual diagram of a dehydrator used in the method for treating sewage sludge according to the present invention.
３ 濃縮機 ９ 脱水機 ９ａ スクリュープレス 3 concentrator 9 dehydrator 9a screw press
Claims (3)
加して凝集処理し、脱水機で脱水処理する汚泥の処理方
法において、下水汚泥の一部に高分子凝集剤を添加して
凝集後、上記汚泥を濃縮機（３）で濃縮し、この濃縮汚
泥と残りの原汚泥とを混合し、上記混合汚泥に高分子凝
集剤を添加して、凝集フロックを生成させ、脱水機
（９）で固液分離処理を行なうことを特徴とする下水汚
泥の処理方法。1. A method for treating sludge, comprising adding a cationic polymer flocculant to sewage sludge to perform coagulation treatment and dehydration treatment with a dehydrator, in which a polymer coagulant is added to a part of the sewage sludge before coagulation. The sludge is concentrated by a thickener (3), the thickened sludge is mixed with the remaining raw sludge, a polymer flocculant is added to the mixed sludge to generate floc, and a dehydrator (9) A method for treating sewage sludge, which comprises performing solid-liquid separation treatment in.
なう汚泥量を原汚泥の全量の５０〜８０％とし、濃縮倍
率を５〜１５倍とすることを特徴とする請求項１に記載
の下水汚泥の処理方法。2. The sewage according to claim 1, wherein in the above treatment method, the amount of sludge to be concentrated is 50 to 80% of the total amount of the original sludge and the concentration ratio is 5 to 15 times. Sludge treatment method.
（９）として圧入式のスクリュープレス（９ａ）や回転
加圧脱水機（９ｂ）等の圧入型脱水機を使用することを
特徴とする請求項１及び請求項２に記載の下水汚泥の処
理方法。3. A press-fitting type dehydrator such as a press-fitting type screw press (9a) or a rotary press dehydrator (9b) is used as the dehydrator (9) for performing solid-liquid separation of the concentrated sludge. The method for treating sewage sludge according to claim 1 or claim 2.
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| JP2001379572A JP3680994B2 (en) | 2001-12-13 | 2001-12-13 | Sewage sludge treatment method |
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