JP2003340205A - Flocculation and separation apparatus - Google Patents
Flocculation and separation apparatusInfo
- Publication number
- JP2003340205A JP2003340205A JP2002154221A JP2002154221A JP2003340205A JP 2003340205 A JP2003340205 A JP 2003340205A JP 2002154221 A JP2002154221 A JP 2002154221A JP 2002154221 A JP2002154221 A JP 2002154221A JP 2003340205 A JP2003340205 A JP 2003340205A
- Authority
- JP
- Japan
- Prior art keywords
- additive
- separation tank
- tank
- sludge
- separated
- 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
- Separation Of Suspended Particles By Flocculating Agents (AREA)
Abstract
Description
【発明の詳細な説明】
【０００１】
【発明の属する技術分野】本発明は、水処理分野におい
て、懸濁物質を凝集分離して処理水質の向上を図る凝集
分離装置に関し、特に添加物回収手段を備える凝集分離
装置に関するものである。
【０００２】
【従来の技術】粒状添加物を用いた凝集分離は高速凝集
処理が可能なため、下水処理の分野で雨天時に増加する
汚水等の直接処理等での利用が検討されている。図２は
粒状添加物を用いた従来の凝集分離装置を示すフロー図
である。同図において、１は原水導入管、２はその原水
導入管１から汚泥等の懸濁物質を含んだ原水を導入する
凝集反応槽であり、この凝集反応槽２には、無機凝集剤
供給手段３および高分子凝集剤供給手段４から無機凝集
剤および高分子凝集剤が添加されると共に、微粒砂等に
粒状添加物も添加されるようになっている。
【０００３】５は前記凝集反応槽２からの流出水を導入
して分離物と処理水とに分離する固液分離槽（沈殿
槽）、６はその固液分離槽５から分離物を引き抜く引抜
手段としてのポンプであり、このポンプ６による引抜物
質は配管７を介して液体サイクロン８に送られるように
なっている。その液体サイクロン８は、前記引抜物質に
含まれる粒状添加物を分離回収し、その回収添加物を凝
集反応槽２に返送すると共に、分離汚泥を系外に排出す
るものである。
【０００４】次に上記従来の凝集分離装置の動作につい
て説明する。原水導入管１から凝集反応槽２内に導入さ
れた原水に無機凝集剤と高分子凝集剤および添加物が添
加されることにより、凝集反応槽２では、原水に含まれ
た懸濁物質などが凝集され、これによって凝集フロック
が生成される。その凝集フロックを含んだ流出水は次の
固液分離槽５に移流し、この固液分離槽５で添加物を含
んだ分離物と処理水とに分離され、処理水は系外に排出
され、分離物はポンプ６で引き抜かれた後、配管７を介
して液体サイクロン８に送られる。この液体サイクロン
８では、固液分離槽５からの引抜物質に含まれた添加物
が分離され、その分離添加物は凝集反応槽２内に返送さ
れて再使用に供せられ、添加物が分離された汚泥は系外
に排出される。
【０００５】
【発明が解決しようとする課題】従来の凝集分離装置は
以上のように構成されているので、高濃度の粒状添加物
を含んだ凝集汚泥が固液分離槽５の底部に溜まった場
合、その固液分離槽５から液体サイクロン８に送られた
引抜物質中の高濃度粒状添加物によって液体サイクロン
８の吐出口が詰まるか、あるいは液体サイクロン８の分
級効率が変化し、その状況によって液体サイクロン８か
らの排出汚泥に粒状添加物が多量に混入する場合があっ
た。また、液体サイクロン８の分級効率は液体サイクロ
ン８の上下の吐出口径比で変化するため、その吐出口径
比によっても液体サイクロン８の分級効率が低下し、液
体サイクロン８からの分離汚泥中に粒状添加物が多量に
混入する場合があり、その結果、液体サイクロン８の下
から吐出する粒状添加物が減少し、処理工程での粒状添
加物不足により処理水質の悪化を来す場合があった。さ
らに、高い粒状添加物回収率を得るには、小径の液体サ
イクロンを高い圧力で使用しなければならないため、液
体サイクロンの台数は増加し、且つ配管７および液体サ
イクロン８のそれぞれの内部が早期摩耗し、それらの交
換頻度が高くなるなどの課題があった。
【０００６】本発明は上記のような課題を解決するため
になされたもので、添加物を含む凝集汚泥を容易且つ効
率的に添加物と分離汚泥とに分離することができる凝集
分離装置を提供することを目的とする。
【０００７】
【課題を解決するための手段】本発明に係る凝集分離装
置は、原水に含まれた懸濁物質等を凝集処理する凝集反
応槽と、この凝集反応槽からの流出水を固液分離する固
液分離槽と、引抜物質を添加物と汚泥に分離する添加物
分離槽と、前記固液分離槽から前記添加物分離槽に引抜
物質を移送する配管とから構成される。前記添加物分離
槽で液体サイクロンのように配管などに圧力をかけるこ
となく添加物を分離して、良好な水質を得るものであ
る。
【０００８】
【発明の実施の形態】以下、本発明の実施の一形態を説
明する。
実施の形態１．図１は本発明の実施の形態１による凝集
分離装置を示すフロー図であり、図２と同一または相当
部分には同一符号を付して重複説明を省略する。なお、
図１には図２に示す無機凝集剤供給手段３および高分子
凝集剤供給手段４を示していないが、それらの無機凝集
剤供給手段３および高分子凝集剤供給手段４を本発明の
凝集反応槽２は備えているものである。
【０００９】図１において、９は凝集反応槽２から混合
物を引き抜く引抜手段としてのポンプ、１０はそのポン
プ９と固液分離槽５の汚泥引抜用ポンプ６との共通の配
管７を介して引抜物質を導入する添加物分離槽である。
なお混合物は凝集反応槽の堆積物を、分離物は固液分離
槽での分離堆積物を、引抜物質は配管で移送される物質
を指す。この添加物分離槽１０は、引抜物質を導入し、
その引抜物質に含まれた添加物を重力により沈降分離さ
せると共に、分離汚泥を系外に排出するもので、添加物
分離槽１０としては、添加物の沈降を促進する円錐形状
のほか四角錐形状などホッパ型や掻寄機型等が挙げられ
る。
【００１０】１１は添加物分離槽１０から添加物を導入
して凝集反応槽２内に供給する添加物供給手段である。
この添加物供給手段１１としては、添加物分離槽１０か
らの自然流下、ポンプ、ベルトコンベア等が挙げられる
が、添加物分離槽１０から凝集反応槽２内に粒状添加物
を移送できるものであれば、如何なるものであってもよ
い。なお、添加物としては、砂または砂に近似する比重
２〜８の範囲である有機系や無機系の物質、または、そ
れらの混合物、例えば微粒砂、酸化ジルコニウムやガー
ネットなどが挙げられる。
【００１１】次に動作について説明する。装置運転中に
おいて、固液分離槽５、凝集反応槽２からポンプ６，９
により引抜物質が引き抜かれ、そのポンプ移送中に、引
抜物質中の添加物から汚泥が剥離することもある。引抜
手段（ポンプ６，９）としては、耐摩耗性の渦巻ポンプ
など、添加物による摩耗を防止できるポンプであれば、
如何なるポンプでもよい。その後、引抜物質は添加物分
離槽１０内に流入する。この添加物分離槽１０では、添
加物が重力で沈降して汚泥と分離され、その分離汚泥は
添加物分離槽１０からの溢出により系外に排出される。
ここで、添加物分離槽１０内での例えば微粒砂の沈降速
度は１４０ｍ／ｈ、汚泥の沈降速度は３〜４ｍ／ｈであ
り、添加物の沈降速度が汚泥の沈降速度に比べ非常に大
きいので、短時間（５分程度）で添加物の沈降が可能で
ある。そして、添加物分離槽１０で沈降分離された添加
物は添加物供給手段１１によって凝集反応槽２内に供給
される。
【００１２】実施例１．次に、上記実施の形態１による
凝集分離装置を実験運転した結果を説明する。
実験条件
原水；下水処理場の最初沈殿池の流入水
原水流量；２８８０ｍ３／日（１２０ｍ３／ｈ）
原水濁度；１００ＮＴＵ
微粒砂；比重２．６、有効径１７０μｍ
無機凝集剤；ＰＡＣ１０ｍｇ／Ｌ（ＡＬ２Ｏ３として）
高分子凝集剤；アニオン系有機高分子１．０ｍｇ／Ｌ
固液分離槽の汚泥引抜手段；ポンプ、循環水量７．２ｍ
３／ｈ
添加物分離槽；滞留時間３ｍｉｎ
【００１３】この実験では、凝集反応槽２に下水処理場
の最初沈殿池の流入水を流入させ、無機凝集剤にＰＡＣ
１０ｍｇ／Ｌ（ＡＬ２Ｏ３）を、高分子凝集剤にアニオ
ン系有機高分子１．０ｍｇ／Ｌを、微粒砂（比重２．
６、有効径１７０μｍ）を注入した。引抜手段として
は、微粒砂スラリー用ポンプを使用し、時間当たり７．
２ｍ３／ｈで運転した。添加物分離槽１０は滞留時間３
ｍｉｎの円錐型の槽を使用した。添加物供給手段１１と
してはベルトコンベアを使用して添加物分離槽１０から
の微粒砂を凝集反応槽２内に供給した。
【００１４】ここで、循環水量および配管内砂濃度一定
での配管径の違いによる処理性能を表１に示す。
【００１５】
【表１】
【００１６】表１に示すように、従来装置では循環ライ
ン配管の径が４０φから６０φになることで配管内流速
が１．６（ｍ／ｈ）から０．７（ｍ／ｈ）となる。この
ことで従来装置のＳＳ除去率は８２（％）から６５
（％）に減少する。しかし、本発明装置では配管内流速
の変化は従来例と同じように１．６（ｍ／ｈ）から０．
７（ｍ／ｈ）に変化したが、ＳＳ除去率は８２（％）と
変化はなかった。このことから、従来装置の場合は汚泥
循環ラインの配管７の流速減少により、液体サイクロン
８の分級効率が低下し、その液体サイクロン８からの分
離汚泥中に微粒砂が流出し、その結果、処理性能［ＳＳ
（浮遊物質）除去率］は低下した。一方、本発明装置で
は循環ラインの配管７の流速が減少しても処理性能には
影響がなかった。
【００１７】次に、循環ラインの配管７内での微粒砂濃
度を変化させて排出汚泥中に含まれる微粒砂濃度を比較
した結果を表２に示す。なお、循環ラインの配管７の配
管径は４０φである。
【００１８】
【表２】
【００１９】表２に示すように、従来装置では配管内微
粒砂濃度が１０，０００から２０，０００（ｍｇ／Ｌ）
に変化すると、分離汚泥中に含まれる微粒砂が５から４
０（ｍｇ／Ｌ）まで変化するが、本発明装置は配管内微
粒砂濃度が同様に変化しても、分離汚泥中に含まれる微
粒砂は５から２０（ｍｇ／Ｌ）までしか変化しなかっ
た。このことから、従来装置は循環ラインの配管７内の
微粒砂濃度が増加すると、液体サイクロン８からの分離
汚泥中に含まれる微粒砂濃度は増加した。一方、本発明
装置は循環ラインの配管７内の微粒砂濃度が増加しても
添加物分離槽１０からの溢出による分離汚泥中の微粒砂
濃度はそれほど増加せず、微粒砂濃度の変動に対しても
十分に対応できることが確認された。
【００２０】次に、連続運転による従来装置と本発明装
置の交換頻度の比較を表３に示す。
【００２１】
【表３】
【００２２】固液分離槽５のポンプ６は、ポンプシール
部、ポンプ本体（インペラ等）、循環ラインの配管７の
交換頻度を比較した結果、表３に示すように、交換頻度
は従来装置と本発明で比較するとポンプシール部が１回
／２４月が１回／３６月になり、ポンプ本体は１回／３
６月が１回／４８月になり、循環ラインの配管は１回／
４８月が１回／６０月になった。このことから本発明装
置は従来装置と比較したいずれの部位においても寿命を
１年以上に延長することができた。また、従来装置と本
発明装置のイニシャルコストを比較した結果を表４に示
す。
【００２３】
【表４】
【００２４】表４に示すようにコスト面を比較すると、
従来装置の液体サイクロンで添加物を引抜物質から分離
する場合は、５Ｌ用で２５０，０００円であるが、本発
明の装置の添加物分離槽は簡単な構造の槽なので、３６
０Ｌ用で５０，０００円で済んだことより、本発明装置
は従来装置の１／５と安価であった。
【００２５】以上説明した実施の形態１によれば、凝集
反応槽２、固液分離槽５からの引抜物質を添加物分離槽
１０に導入して前記引抜物質に含まれる添加物を重力に
より沈降分離させ、その分離添加物を凝集反応槽２内に
供給すると共に、分離汚泥を前記添加物分離槽１０から
の溢出により系外に排出する構成としたので、従来例の
液体サイクロンのように分級効率が変化するようなこと
がなく、添加物分離槽１０からの分離汚泥中に粒状添加
物が多量に混入するようなことがない。したがって、添
加物分離槽１０の下部から吐出する添加物が大きく減少
するようなことがなく、凝集反応槽２での粒状添加物不
足に起因した処理水質の悪化を防止でき、常に安定した
処理水質を得ることができるという効果がある。
【００２６】ここで、従来例の液体サイクロン８の場
合、循環ラインの配管７内の流速が減少して分級効率が
悪くなるため、液体サイクロン８からの分離汚泥中に微
粒砂が流出して添加物が不足することで処理性能が悪化
していたが、本発明の添加物分離槽１０によれば、添加
物の沈降速度が汚泥の沈降速度よりも非常に速いことを
利用しているので、添加物分離槽１０からの溢出により
系外に排出される分離汚泥中に添加物が多量に混入する
ようなことはない。したがって、循環ラインの配管７の
流速が減少しても処理性能に影響を及ぼすことがないと
いう効果がある。
【００２７】また、本発明によれば、循環ラインの配管
７内の流速変動や微粒砂濃度の変動に十分対応でき、循
環ラインの配管７内を低圧力に維持できるため、汚泥引
抜ポンプ６，９のポンプシール部やポンプ本体（インペ
ラ等）、循環ラインの配管７の交換頻度を少なくでき、
イニシャルコストを大幅に縮減できるという効果があ
る。
【００２８】
【発明の効果】以上のように本発明によれば、添加物使
用による凝集分離装置において、原水中の懸濁物質を凝
集処理する凝集反応槽と、この凝集反応槽から流出水を
導入して分離物と処理水とに分離する固液分離槽と、こ
の固液分離槽、前記凝集反応槽から引抜物質を引き抜く
引抜手段と、この引抜手段で引き抜いた引抜物質を導入
し、その引抜物質中の添加物を分離する添加物分離槽と
を備え、その添加物分離槽で分離された添加物を凝集反
応槽内に供給するように構成したので、従来例の液体サ
イクロンのように分級効率が変化せず、添加物分離槽か
らの分離汚泥中に粒状添加物が多量に混入するようなこ
とがなくなる。このため、添加物分離槽の下部から吐出
する添加物が大きく減少するようなことがなく、凝集反
応槽での粒状添加物不足に起因した処理水質の悪化を防
止でき、常に安定した処理水質を得ることができるとい
う効果がある。
【００２９】また、従来例の場合、循環ラインの配管の
流速減少により、液体サイクロンの分級効率が悪くな
り、液体サイクロンからの分離排出汚泥中に微粒砂が流
出し、処理性能が低下していたが、本発明装置は循環ラ
インの配管の流速が減少しても処理性能には影響がな
い。これは、添加物分離槽が添加物の沈降速度が汚泥の
沈降速度よりも非常に早いことを利用していることによ
る。したがって、添加物を含む引抜物質を容易かつ効率
的に添加物と分離汚泥とに分離できるという効果があ
る。
【００３０】また、循環ラインの配管内の圧力を低圧で
運転しても、分離汚泥中に含まれる添加物濃度に大きな
変化はないので、摩耗によるポンプ本体、ポンプの部
品、その他配管などの交換にかかるランニングコストを
小さくできるという効果がある。また、従来装置のよう
に高価な液体サイクロンを用いなくても同等以上の処理
性能が得られるだけでなく、分離汚泥中の添加物濃度を
低濃度に保持できる簡単な添加物分離槽でよいのでイニ
シャルコストも安価で従来の１／５ですむという効果が
ある。Description: BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention relates to a coagulation / separation apparatus for improving the quality of treated water by coagulating / separating suspended substances in the field of water treatment. And a coagulation / separation device comprising: 2. Description of the Related Art Since coagulation separation using a particulate additive enables high-speed coagulation treatment, its use in the field of sewage treatment for direct treatment of sewage and the like that increases in rainy weather is being studied. FIG. 2 is a flowchart showing a conventional coagulation / separation apparatus using a particulate additive. In FIG. 1, reference numeral 1 denotes a raw water introduction pipe, and 2 denotes a coagulation reaction tank for introducing raw water containing suspended substances such as sludge from the raw water introduction pipe 1. The inorganic flocculant and the polymer flocculant are added from the polymer flocculant 3 and the polymer flocculant supplying means 4, and at the same time, granular additives are added to the fine sand or the like. [0005] 5 is a solid-liquid separation tank (sedimentation tank) for introducing the effluent from the agglutination reaction tank 2 to separate the separated substance and treated water, and 6 is a pull-out for extracting the separated substance from the solid-liquid separation tank 5. This is a pump as a means, and a substance to be withdrawn by the pump 6 is sent to a liquid cyclone 8 via a pipe 7. The liquid cyclone 8 separates and collects the particulate additive contained in the extracted material, returns the collected additive to the coagulation reaction tank 2, and discharges the separated sludge to the outside of the system. Next, the operation of the above-mentioned conventional coagulation / separation apparatus will be described. By adding an inorganic coagulant, a polymer coagulant, and additives to raw water introduced into the coagulation reaction tank 2 from the raw water introduction pipe 1, suspended substances contained in the raw water are added to the coagulation reaction tank 2. Agglomerated, thereby producing agglomerated flocs. The effluent containing the flocculent flocks is transferred to the next solid-liquid separation tank 5, where it is separated into a separated product containing additives and treated water, and the treated water is discharged out of the system. After being separated by a pump 6, the separated material is sent to a liquid cyclone 8 via a pipe 7. In this liquid cyclone 8, additives contained in the substance to be withdrawn from the solid-liquid separation tank 5 are separated, and the separated additives are returned to the coagulation reaction tank 2 for reuse, and the additives are separated. The sludge is discharged out of the system. [0005] Since the conventional coagulation / separation apparatus is configured as described above, coagulated sludge containing a high concentration of particulate additives accumulates at the bottom of the solid-liquid separation tank 5. In this case, the discharge outlet of the liquid cyclone 8 is clogged by the high-concentration particulate additive in the withdrawn material sent from the solid-liquid separation tank 5 to the liquid cyclone 8, or the classification efficiency of the liquid cyclone 8 changes. In some cases, a large amount of the particulate additive was mixed in the sludge discharged from the liquid cyclone 8. In addition, since the classification efficiency of the hydrocyclone 8 changes depending on the upper and lower discharge port diameter ratios of the liquid cyclone 8, the classification efficiency of the liquid cyclone 8 is also reduced by the discharge port diameter ratio, and granular addition into the sludge separated from the liquid cyclone 8 is performed. In some cases, a large amount of substances may be mixed in, and as a result, the amount of the particulate additive discharged from below the liquid cyclone 8 may decrease, and the quality of the treated water may deteriorate due to the lack of the particulate additive in the treatment process. Furthermore, in order to obtain a high particulate additive recovery rate, a small-diameter hydrocyclone must be used at a high pressure, so that the number of hydrocyclones increases, and the inside of each of the pipe 7 and the hydrocyclone 8 is rapidly worn. However, there has been a problem that the frequency of exchanging them increases. SUMMARY OF THE INVENTION The present invention has been made to solve the above-mentioned problems, and provides a coagulation / separation apparatus capable of easily and efficiently separating coagulated sludge containing additives into additives and separated sludge. The purpose is to do. A coagulation / separation apparatus according to the present invention comprises a coagulation reaction tank for coagulating a suspended substance or the like contained in raw water, and a solid-liquid effluent from the coagulation reaction tank. It comprises a solid-liquid separation tank for separation, an additive separation tank for separating the extracted substance into additives and sludge, and a pipe for transferring the extracted substance from the solid-liquid separation tank to the additive separation tank. In the additive separation tank, additives are separated without applying pressure to pipes or the like as in a liquid cyclone, and good water quality is obtained. An embodiment of the present invention will be described below. Embodiment 1 FIG. FIG. 1 is a flowchart showing a coagulation / separation apparatus according to Embodiment 1 of the present invention. The same or corresponding parts as those in FIG. In addition,
FIG. 1 does not show the inorganic flocculant supply means 3 and the polymer flocculant supply means 4 shown in FIG. The tank 2 is provided. In FIG. 1, reference numeral 9 denotes a pump as a drawing means for pulling out a mixture from the flocculation reaction tank 2, and reference numeral 10 denotes a drawing through a common pipe 7 between the pump 9 and a sludge drawing pump 6 of the solid-liquid separation tank 5. An additive separation tank for introducing a substance.
Note that the mixture refers to the sediment in the agglutination reaction tank, the separated substance refers to the separated sediment in the solid-liquid separation tank, and the withdrawn substance refers to the substance transferred by piping. This additive separation tank 10 introduces a withdrawn substance,
The additive contained in the extracted material is settled and separated by gravity, and the separated sludge is discharged out of the system. The additive separation tank 10 has a conical shape for promoting the sedimentation of the additive, and a quadrangular pyramid shape. Hopper type and scraper type. Reference numeral 11 denotes an additive supply means for introducing an additive from the additive separation tank 10 and supplying the additive into the coagulation reaction tank 2.
Examples of the additive supply means 11 include a natural flow from the additive separation tank 10, a pump, a belt conveyor, and the like. Any means capable of transferring the particulate additive from the additive separation tank 10 into the agglutination reaction tank 2 may be used. Any type may be used. Examples of the additive include sand or an organic or inorganic substance having a specific gravity in the range of 2 to 8, which is close to that of sand, or a mixture thereof, for example, fine sand, zirconium oxide, garnet, and the like. Next, the operation will be described. During the operation of the apparatus, pumps 6 and 9 are supplied from the solid-liquid separation tank 5 and the coagulation reaction tank 2.
As a result, the extracted material is withdrawn, and during the pumping, the sludge may be separated from the additives in the withdrawn material. As a drawing means (pumps 6 and 9), if the pump can prevent wear by additives, such as a wear-resistant centrifugal pump,
Any pump may be used. Thereafter, the withdrawn material flows into the additive separation tank 10. In the additive separating tank 10, the additive settles by gravity and is separated from sludge, and the separated sludge is discharged out of the system by overflow from the additive separating tank 10.
Here, for example, the sedimentation speed of the fine sand in the additive separation tank 10 is 140 m / h, the sedimentation speed of the sludge is 3 to 4 m / h, and the sedimentation speed of the additive is much higher than the sedimentation speed of the sludge. Therefore, it is possible to settle the additive in a short time (about 5 minutes). The additive separated and settled in the additive separation tank 10 is supplied into the agglutination reaction tank 2 by the additive supply means 11. Embodiment 1 FIG. Next, the results of the experimental operation of the coagulation / separation apparatus according to the first embodiment will be described. Influent raw water flow rate of the primary sedimentation of sewage treatment plant; experimental conditions raw 2880m 3 / day (120m 3 / h) raw turbidity; 100 NTU fine sand; specific gravity 2.6, the effective diameter 170μm inorganic coagulant; PAC10mg / L (As AL 2 O 3 ) Polymer flocculant; anionic organic polymer 1.0 mg / L Sludge extraction means for solid-liquid separation tank; pump, circulating water amount 7.2 m
3 / h Additive separation tank; residence time 3 min In this experiment, the inflow water of the first sedimentation basin of the sewage treatment plant was flowed into the coagulation reaction tank 2 and the PAC was added to the inorganic coagulant.
10 mg / L (AL 2 O 3 ), an anionic organic polymer 1.0 mg / L as a polymer flocculant, and fine sand (specific gravity 2.
6, effective diameter 170 μm). As a drawing means, a pump for fine sand slurry is used, and 7.
The operation was performed at 2 m 3 / h. The additive separation tank 10 has a residence time of 3
A min-shaped conical tank was used. As the additive supply means 11, a fine-grained sand from the additive separation tank 10 was supplied into the coagulation reaction tank 2 using a belt conveyor. Table 1 shows the treatment performance depending on the pipe diameter when the amount of circulating water and the sand concentration in the pipe are constant. [Table 1] As shown in Table 1, in the conventional apparatus, the flow rate in the pipe is changed from 1.6 (m / h) to 0.7 (m / h) by changing the diameter of the circulation line pipe from 40 φ to 60 φ. As a result, the SS removal rate of the conventional device is 82 (%) to 65
(%). However, in the apparatus of the present invention, the change of the flow velocity in the pipe is changed from 1.6 (m / h) to 0.1 as in the conventional example.
Although it changed to 7 (m / h), the SS removal rate did not change to 82 (%). From this, in the case of the conventional apparatus, the classification efficiency of the liquid cyclone 8 is reduced due to the decrease in the flow velocity of the pipe 7 of the sludge circulation line, and the fine sand flows out into the separated sludge from the liquid cyclone 8, and as a result, Performance [SS
(Suspended matter) removal rate]. On the other hand, in the apparatus of the present invention, the processing performance was not affected even if the flow velocity in the circulation line pipe 7 was reduced. Next, Table 2 shows the results of comparison of the concentration of the fine sand contained in the discharged sludge by changing the concentration of the fine sand in the piping 7 of the circulation line. In addition, the piping diameter of the piping 7 of the circulation line is 40φ. [Table 2] As shown in Table 2, in the conventional apparatus, the fine sand concentration in the pipe was 10,000 to 20,000 (mg / L).
The fine sand contained in the separated sludge changes from 5 to 4
Although it changes to 0 (mg / L), even if the fine sand concentration in the pipe similarly changes, the fine sand contained in the separated sludge changes only from 5 to 20 (mg / L). Was. For this reason, in the conventional apparatus, when the concentration of the fine sand in the pipe 7 of the circulation line increased, the concentration of the fine sand contained in the sludge separated from the liquid cyclone 8 increased. On the other hand, in the apparatus of the present invention, even if the fine sand concentration in the circulation line pipe 7 increases, the fine sand concentration in the separated sludge due to the overflow from the additive separation tank 10 does not increase so much. It was confirmed that they could be adequately dealt with. Next, Table 3 shows a comparison of the frequency of replacement between the conventional apparatus and the apparatus of the present invention in continuous operation. [Table 3] As a result of comparing the replacement frequency of the pump seal portion, the pump body (impeller and the like), and the piping 7 of the circulation line, as shown in Table 3, the replacement frequency of the pump 6 of the solid-liquid separation tank 5 is the same as that of the conventional device. In comparison with the present invention, the pump seal portion is once / 24 months is once / 36 months, and the pump body is once / 3 times.
June is once / 48 months, and circulation line piping is once /
48 months was once / 60 months. From this, the device of the present invention was able to extend the service life to one year or more at any part as compared with the conventional device. Table 4 shows the results of comparing the initial costs of the conventional apparatus and the apparatus of the present invention. [Table 4] As shown in Table 4, the costs are compared.
When the additive is separated from the withdrawn material by the liquid cyclone of the conventional apparatus, the price is 250,000 yen for 5 L. However, since the additive separation tank of the apparatus of the present invention has a simple structure, it is 36 yen.
The device of the present invention was as inexpensive as 1/5 that of the conventional device, because the cost for 0L was 50,000 yen. According to the first embodiment described above, the substances extracted from the coagulation reaction tank 2 and the solid-liquid separation tank 5 are introduced into the additive separation tank 10, and the additives contained in the extracted substances are settled by gravity. Separation is performed, the separated additive is supplied into the coagulation reaction tank 2, and the separated sludge is discharged out of the system by overflow from the additive separation tank 10. Therefore, classification is performed as in the conventional liquid cyclone. Efficiency does not change, and a large amount of particulate additive is not mixed into the separated sludge from the additive separation tank 10. Therefore, the additive discharged from the lower part of the additive separation tank 10 does not greatly decrease, and it is possible to prevent the deterioration of the treatment water quality due to the shortage of the particulate additive in the agglutination reaction tank 2 and to always maintain the stable treatment water quality. Is obtained. Here, in the case of the conventional liquid cyclone 8, since the flow velocity in the circulation line pipe 7 is reduced and the classification efficiency is deteriorated, fine sand flows out into the sludge separated from the liquid cyclone 8 and is added. Although the treatment performance deteriorated due to the shortage of the material, the additive separation tank 10 of the present invention utilizes that the sedimentation speed of the additive is much faster than the sedimentation speed of the sludge. A large amount of additive is not mixed into the separated sludge discharged out of the system due to overflow from the additive separation tank 10. Therefore, there is an effect that the processing performance is not affected even if the flow velocity of the circulation line piping 7 decreases. Further, according to the present invention, it is possible to sufficiently cope with fluctuations in flow velocity and fine sand concentration in the circulation line piping 7 and to maintain the inside of the circulation line piping 7 at a low pressure. 9, the frequency of replacing the pump seal part, the pump body (impeller, etc.) and the circulation line piping 7 can be reduced.
There is an effect that the initial cost can be significantly reduced. As described above, according to the present invention, in an aggregating / separating apparatus using an additive, an agglutination reaction tank for aggregating a suspended substance in raw water, and an effluent from the agglutination reaction tank are removed. A solid-liquid separation tank to be introduced and separated into a separated product and treated water, and the solid-liquid separation tank, extraction means for extracting the extracted substance from the agglutination reaction tank, and the extracted substance extracted by the extraction means are introduced. An additive separation tank that separates the additives in the extracted material is provided, and the additives separated in the additive separation tank are configured to be supplied into the agglutination reaction tank. The classification efficiency does not change, and a large amount of the particulate additive is not mixed into the sludge separated from the additive separation tank. For this reason, the additive discharged from the lower part of the additive separation tank does not significantly decrease, and it is possible to prevent the deterioration of the treatment water quality due to the shortage of the particulate additive in the flocculation reaction tank, and to always maintain the stable treatment water quality. There is an effect that it can be obtained. Further, in the case of the conventional example, the classification efficiency of the hydrocyclone is deteriorated due to the decrease in the flow velocity of the piping of the circulation line, and fine sand flows out into the separated and discharged sludge from the hydrocyclone, and the treatment performance is reduced. However, the apparatus of the present invention does not affect the processing performance even if the flow velocity of the circulation line piping is reduced. This is due to the fact that the additive separation tank utilizes that the sedimentation speed of the additive is much faster than the sedimentation speed of the sludge. Therefore, there is an effect that the extracted material containing the additive can be easily and efficiently separated into the additive and the separated sludge. Further, even if the pressure in the circulation line pipe is operated at a low pressure, there is no significant change in the concentration of additives contained in the separated sludge, so that the pump body, pump parts, and other pipes are replaced due to wear. Has the effect of reducing the running cost of In addition, not only the same or higher processing performance can be obtained without using expensive liquid cyclone as in the conventional apparatus, but also a simple additive separation tank that can maintain the additive concentration in the separated sludge at a low concentration is sufficient. The effect is that the initial cost is low and only 1/5 of the conventional one is required.
【図面の簡単な説明】
【図１】本発明の実施の形態１による凝集分離装置を示
すフロー図である。
【図２】従来の凝集沈殿処理装置を概略的に示すフロー
図である。
【符号の説明】
１ 原水導入管
２ 凝集反応槽
３ 無機凝集剤供給手段
４ 高分子凝集剤供給手段
５ 固液分離槽
６ ポンプ（引抜手段）
７ 配管（汚泥循環ライン配管）
９ ポンプ（引抜手段）
１０ 添加物分離槽
１１ 添加物供給手段BRIEF DESCRIPTION OF THE DRAWINGS FIG. 1 is a flowchart showing a coagulation / separation apparatus according to Embodiment 1 of the present invention. FIG. 2 is a flowchart schematically showing a conventional coagulation / sedimentation treatment apparatus. [Description of Signs] 1 Raw water introduction pipe 2 Coagulation reaction tank 3 Inorganic coagulant supply means 4 Polymer coagulant supply means 5 Solid-liquid separation tank 6 Pump (pull-out means) 7 Pipe (sludge circulation line pipe) 9 Pump (pull-out means) 10) Additive separation tank 11 Additive supply means
───────────────────────────────────────────────────── フロントページの続き (72)発明者 菅原 良行 東京都港区芝浦三丁目六番18号 株式会社 西原環境衛生研究所内 (72)発明者 品田 司 東京都港区芝浦三丁目六番18号 株式会社 西原環境衛生研究所内 (72)発明者 間瀬 博子 東京都港区芝浦三丁目六番18号 株式会社 西原環境衛生研究所内 ────────────────────────────────────────────────── ─── Continuation of front page (72) Inventor Yoshiyuki Sugawara 3-6-18 Shibaura, Minato-ku, Tokyo Co., Ltd. Nishihara Environmental Health Research Institute (72) Inventor Tsukasa Shinada 3-6-18 Shibaura, Minato-ku, Tokyo Co., Ltd. Nishihara Environmental Health Research Institute (72) Inventor Hiroko Mase 3-6-18 Shibaura, Minato-ku, Tokyo Co., Ltd. Nishihara Environmental Health Research Institute
Claims (1)
と、この凝集反応槽からの流出水を固液分離する固液分
離槽と、引抜物質を添加物と汚泥に分離する添加物分離
槽と、前記固液分離槽から前記添加物分離槽に引抜物質
を移送する配管とを備えたことを特徴とする凝集分離装
置。Claims: 1. An agglutination reaction tank for aggregating a suspended substance or the like, a solid-liquid separation tank for solid-liquid separation of effluent from the agglutination reaction tank, and an extraction agent containing sludge and an additive. An agglomeration separation device, comprising: an additive separation tank for separating the extracted material; and a pipe for transferring a withdrawn substance from the solid-liquid separation tank to the additive separation tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002154221A JP4004856B2 (en) | 2002-05-28 | 2002-05-28 | Coagulation separation device |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2002154221A JP4004856B2 (en) | 2002-05-28 | 2002-05-28 | Coagulation separation device |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JP2003340205A true JP2003340205A (en) | 2003-12-02 |
| JP4004856B2 JP4004856B2 (en) | 2007-11-07 |
Family
ID=29771072
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|---|---|---|---|
| JP2002154221A Expired - Fee Related JP4004856B2 (en) | 2002-05-28 | 2002-05-28 | Coagulation separation device |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JP4004856B2 (en) |
-
2002
- 2002-05-28 JP JP2002154221A patent/JP4004856B2/en not_active Expired - Fee Related
Also Published As
| Publication number | Publication date |
|---|---|
| JP4004856B2 (en) | 2007-11-07 |
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