JPH02284604A - Solid-liquid separation for waste water - Google Patents
Solid-liquid separation for waste waterInfo
- Publication number
- JPH02284604A JPH02284604A JP11006689A JP11006689A JPH02284604A JP H02284604 A JPH02284604 A JP H02284604A JP 11006689 A JP11006689 A JP 11006689A JP 11006689 A JP11006689 A JP 11006689A JP H02284604 A JPH02284604 A JP H02284604A
- Authority
- JP
- Japan
- Prior art keywords
- liquid separation
- solid
- flow
- waste water
- wastewater
- 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
- 239000007788 liquid Substances 0.000 title claims abstract description 45
- 239000002351 wastewater Substances 0.000 title claims abstract description 43
- 238000000926 separation method Methods 0.000 title claims abstract description 38
- 239000010802 sludge Substances 0.000 abstract description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 abstract description 23
- 238000012423 maintenance Methods 0.000 abstract description 3
- 238000004065 wastewater treatment Methods 0.000 abstract 1
- 230000000694 effects Effects 0.000 description 8
- 238000004140 cleaning Methods 0.000 description 7
- 238000005345 coagulation Methods 0.000 description 7
- 230000015271 coagulation Effects 0.000 description 7
- 238000005189 flocculation Methods 0.000 description 7
- 230000016615 flocculation Effects 0.000 description 7
- 238000004062 sedimentation Methods 0.000 description 7
- 238000011001 backwashing Methods 0.000 description 3
- 230000007423 decrease Effects 0.000 description 3
- 239000010419 fine particle Substances 0.000 description 3
- 238000012545 processing Methods 0.000 description 3
- 238000005406 washing Methods 0.000 description 3
- 230000015572 biosynthetic process Effects 0.000 description 2
- 238000010586 diagram Methods 0.000 description 2
- 230000005484 gravity Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 238000000034 method Methods 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 230000002265 prevention Effects 0.000 description 2
- 239000004576 sand Substances 0.000 description 2
- 230000008093 supporting effect Effects 0.000 description 2
- VEXZGXHMUGYJMC-UHFFFAOYSA-M Chloride anion Chemical compound [Cl-] VEXZGXHMUGYJMC-UHFFFAOYSA-M 0.000 description 1
- 229910021578 Iron(III) chloride Inorganic materials 0.000 description 1
- 238000009825 accumulation Methods 0.000 description 1
- 238000004220 aggregation Methods 0.000 description 1
- 230000002776 aggregation Effects 0.000 description 1
- DIZPMCHEQGEION-UHFFFAOYSA-H aluminium sulfate (anhydrous) Chemical compound [Al+3].[Al+3].[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O.[O-]S([O-])(=O)=O DIZPMCHEQGEION-UHFFFAOYSA-H 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 1
- 239000003830 anthracite Substances 0.000 description 1
- 239000000701 coagulant Substances 0.000 description 1
- 230000008021 deposition Effects 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 239000000945 filler Substances 0.000 description 1
- 238000001914 filtration Methods 0.000 description 1
- 230000003311 flocculating effect Effects 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- RBTARNINKXHZNM-UHFFFAOYSA-K iron trichloride Chemical compound Cl[Fe](Cl)Cl RBTARNINKXHZNM-UHFFFAOYSA-K 0.000 description 1
- 239000000314 lubricant Substances 0.000 description 1
- 238000011056 performance test Methods 0.000 description 1
- 229920000642 polymer Polymers 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 238000009287 sand filtration Methods 0.000 description 1
- 229920006395 saturated elastomer Polymers 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
Abstract
Description
【発明の詳細な説明】
℃産業上の利用分野〕
本発明は廃水の固液分離装置に係り、特に竪型固液分離
ＦＷを用いた廃水の固液分離装置に関する。DETAILED DESCRIPTION OF THE INVENTION Field of industrial application] The present invention relates to a solid-liquid separation device for wastewater, and particularly to a solid-liquid separation device for wastewater using a vertical solid-liquid separation FW.
廃水の固液分離装置として、凝集沈ｌｉｄ ｌ ｆｔ
、砂ろ過装置が一般に用いられている。しかし、凝集沈
澱装置は水面積負荷が１〜２ｍ／ｈと小さいため設置面
債は非常に大きくなり、都市部では好ましくない。また
、砂ろ過方法はろ過速度がすＪ集沈殿装首に比較して５
〜１０ ｍ／ ｈと大きいが、更にコンパクト化を図る
為には高速化が望まれている。そこで、特公昭６１−１
９２６５号公報で１ま廃水の固液分ｔｓ、装置が提案さ
れている（第４図）。As a solid-liquid separation device for wastewater, coagulation sedimentation lid l ft
, sand filters are commonly used. However, since the coagulation-sedimentation apparatus has a small water area load of 1 to 2 m/h, the installation space is very large, which is not preferable in urban areas. In addition, the sand filtration method has a filtration speed of 5.5 compared to the J sedimentation neck.
Although it is large at ~10 m/h, it is desired to increase the speed in order to make it even more compact. Therefore, special public service 1986-1
Japanese Patent No. 9265 proposes an apparatus for controlling the solid-liquid content of wastewater (Fig. 4).
第４図の固液分離装置は水槽５０に、ろ材γ５２と沈、
股部５４とを設けた点を特徴としている。The solid-liquid separator shown in FIG.
It is characterized by the provision of a crotch portion 54.
廃水は廃水流入口５６から渦巻き流５８が生じるよう水
槽５０に導入され、廃水中の粗大フロ 、７りま渦巻き
流の遠心力によって水と分離し、沈降して水槽５０の底
部に沈殿する。そして、廃水は水槽５０の上向流となっ
て回転筒体６０に至り、先ず、回転筒体６０の周面に形
成されたフィルタ６２でろ過される。次いで、回転筒体
６０内部のる材層５２によって更にろ過され処理水とな
り、流出管６３から排出される。フィルタ６２及びろ材
層５２の洗浄は洗浄水を流入管６３から回転筒体６０内
に供給すると共に回転ハンドル６４で回転筒体６０を回
転させ、回転ブラシ６５でフィルタ６２の洗浄を行う。The wastewater is introduced into the water tank 50 from the wastewater inlet 56 so that a swirling flow 58 is generated, and the coarse floc in the wastewater is separated from water by the centrifugal force of the swirling flow, and settles to the bottom of the water tank 50. Then, the wastewater flows upward from the water tank 50 and reaches the rotary cylinder body 60, where it is first filtered by a filter 62 formed on the circumferential surface of the rotary cylinder body 60. Next, the treated water is further filtered by the material layer 52 inside the rotary cylinder 60 and is discharged from the outflow pipe 63. To clean the filter 62 and the filter medium layer 52, cleaning water is supplied from the inflow pipe 63 into the rotary cylinder body 60, the rotary cylinder body 60 is rotated with the rotation handle 64, and the filter 62 is cleaned with the rotary brush 65.
洗浄廃水は水槽５０内を通り、沈降汚泥排出管６６から
水槽５０外へ排出される。The cleaning wastewater passes through the water tank 50 and is discharged to the outside of the water tank 50 from the settled sludge discharge pipe 66.
しかしながら、前記固液分離装置では、廃水の濁質濃度
が高い場合にはる材層５２が短時間で目詰まりし、洗浄
頻度が高くなるという欠点がある。However, the solid-liquid separator has a drawback that when the wastewater has a high turbidity concentration, the lubricant layer 52 becomes clogged in a short period of time, which increases the frequency of cleaning.
このため、処理効率が著しく低下する。また、回転筒体
６０、ブラシ６５等の機械装置部を有するため保守管理
が煩雑となる間頭がある。As a result, processing efficiency is significantly reduced. Furthermore, since it includes mechanical devices such as the rotating cylinder 60 and the brush 65, maintenance management becomes complicated.
本発明はこのような事情に鑑みてなされたもので、処理
場の省スペース化を図ることができると共に、処理水の
水質を高めることのできる廃水の固液分離装置を提供す
ることを目的とする。The present invention was made in view of the above circumstances, and an object of the present invention is to provide a solid-liquid separation device for wastewater that can save space in a treatment plant and improve the quality of treated water. do.
〔課題を解決するための手段〕
本発明は前記目的を達成するために、凝集剤を添加混合
した廃水を円筒型固液分離槽の中間位置に旋回上向流で
流入させ、前記円筒型固液分離槽の下部にフロック沈降
部を形成すると共に前記廃水の流入口上方に固液分離槽
の横断方向に整流板を配置したことを特徴としている。[Means for Solving the Problems] In order to achieve the above-mentioned object, the present invention causes wastewater mixed with a flocculant to flow into an intermediate position of a cylindrical solid-liquid separation tank in a swirling upward flow. The present invention is characterized in that a floc settling section is formed in the lower part of the liquid separation tank, and a rectifying plate is arranged in the transverse direction of the solid-liquid separation tank above the inlet of the waste water.
本発明によれば、廃水に凝集剤（２４）を添加すると共
に、廃水を円筒型固液分離槽（１２）内に接線方向に導
入し旋回流を形成するようにしている。そして、旋回流
によって生じる遠心力でフロックを粗分離しながら液を
上方に導き、上方に設けられた整流板（１４）によって
スラッジブランケットＦＡ’ （３１）を形成するよう
にしている。According to the present invention, a flocculant (24) is added to the wastewater, and the wastewater is introduced tangentially into the cylindrical solid-liquid separation tank (12) to form a swirling flow. The flocs are roughly separated by the centrifugal force generated by the swirling flow while the liquid is guided upward, and a sludge blanket FA' (31) is formed by the baffle plate (14) provided above.
この整流板（１４）は旋回流を整流しフロックの沈降分
離を促進すると共に、上方に形成されるスラッジブラン
ケット層（３１）の沈降を阻°止する。The current plate (14) rectifies the swirling flow to promote sedimentation and separation of flocs, and also prevents the sludge blanket layer (31) formed above from settling.
また、スラッジブランケット層（３１）を廃水が通過す
ることにより、廃水中のフロックが捕捉される。スラッ
ジブランケット層（３１）上方のろ材層（１６）は、ス
ラッジブランケット層（３１）を通過したフロックをさ
らに捕捉し、除去する機能を有する。Furthermore, flocs in the wastewater are captured by the wastewater passing through the sludge blanket layer (31). The filter layer (16) above the sludge blanket layer (31) has the function of further trapping and removing flocs that have passed through the sludge blanket layer (31).
以下、添付図面に従って本発明に係る廃水の固液分離装
置の好ましい実施例を詳説する。Hereinafter, preferred embodiments of the solid-liquid separation device for wastewater according to the present invention will be described in detail with reference to the accompanying drawings.
第１図は本発明に係る固液分離装置の概略を示す系統図
である。第１図の固液分離装置は凝集槽１０、固液分離
槽１２、整流板１４、ろ材層１６を主な構成部材として
いる。凝集槽１０には廃水を供給する導入管２０が接続
されている。また、凝集剤２４、さらに、必要に応じて
凝集助剤２６が凝集槽１０に添加される。凝集剤２４に
は硫酸バンド、ポリ塩化アルミ、塩化第２鉄等の無機凝
集剤、凝集助剤２６にはアニオン性又はノニオン性の高
分子凝集剤が好適である。FIG. 1 is a system diagram schematically showing a solid-liquid separation apparatus according to the present invention. The solid-liquid separator shown in FIG. 1 has a coagulation tank 10, a solid-liquid separation tank 12, a current plate 14, and a filter layer 16 as main components. An introduction pipe 20 for supplying waste water is connected to the coagulation tank 10. Further, a flocculant 24 and, if necessary, a flocculation aid 26 are added to the flocculation tank 10. The flocculant 24 is preferably an inorganic flocculant such as aluminum sulfate, polyaluminum chloride, or ferric chloride, and the flocculant 26 is preferably an anionic or nonionic polymer flocculant.
凝集槽１０と固液分離槽１２とは廃水供給管２８で接続
される。The flocculation tank 10 and the solid-liquid separation tank 12 are connected by a wastewater supply pipe 28.
第２図は円筒型固液分離槽１２における前記廃水供給管
２８近傍の内部構造を示す断面図である。FIG. 2 is a sectional view showing the internal structure of the cylindrical solid-liquid separation tank 12 in the vicinity of the wastewater supply pipe 28.
第１図及び第２図に示すように、円筒型固液分離槽１２
の略中央部には内筒３２が図示しないリブ等によって支
持されている。また、廃水供給管２８は第２図に示され
るように円筒型面液分離槽１２の接線方向の位置に接続
され、導入された廃水は円形型固液分離槽１２内で矢印
に示すよう第２図上で旋回流が生じるよう導入される。As shown in FIGS. 1 and 2, a cylindrical solid-liquid separation tank 12
An inner cylinder 32 is supported by a rib (not shown) or the like approximately in the center of the cylinder. The waste water supply pipe 28 is connected to the tangential direction of the cylindrical solid-liquid separation tank 12 as shown in FIG. The flow is introduced so as to generate a swirling flow as shown in Fig. 2.
また、円筒型固液分離槽１２は下部に於いて逆円錐形の
フロック沈降部１２Ａが形成されており、その下端部に
沈降汚泥排出管３３が接続されている。Further, the cylindrical solid-liquid separation tank 12 has an inverted conical floc settling section 12A formed at its lower part, and a settled sludge discharge pipe 33 is connected to the lower end thereof.
廃水供給管２８の上方にはスラッジブランケット層３１
を形成するため整流板１４が取り付けられる。第３図は
整流板１４の構造を示す斜視図である。第３図に示すよ
うに、整流板１４は板格子状に形成されている。整流板
１４は供給管２８の流入口３０から上方に設置されてい
る。整流板１４の取付は位置は流入口３０の上方より、
筒径Ｘ（１〜３）倍が好ましい。この値が１以下では、
前記接線方向流入による旋回流フロキュレーション作用
が不十分となりフロック沈降部での濁質捕捉率が低下す
る。またこの値が３以上では槽高がいたずらに高くなり
、格別の効果なく、装置の大型化につながり、非効率と
なる。整流板１４の開孔率は６０〜８０％が望ましい。Above the wastewater supply pipe 28 is a sludge blanket layer 31.
A rectifying plate 14 is attached to form a current. FIG. 3 is a perspective view showing the structure of the current plate 14. As shown in FIG. 3, the current plate 14 is formed in a plate lattice shape. The current plate 14 is installed above the inlet 30 of the supply pipe 28 . The current plate 14 is installed from above the inlet 30.
The cylinder diameter is preferably X (1 to 3) times. If this value is less than 1,
The swirling flow flocculation effect due to the tangential inflow becomes insufficient, and the turbidity capture rate in the floc settling section decreases. Moreover, if this value is 3 or more, the height of the tank becomes unnecessarily high, and there is no particular effect, leading to an increase in the size of the apparatus, resulting in inefficiency. The aperture ratio of the current plate 14 is preferably 60 to 80%.
開口率６０％以下では整流板１４を通る水の流速が過大
となり、その衝撃力で整流板１４のフロックを破損させ
る現象がみられる。また整流板１４近傍での層流状態が
乱れ、フロック生成作用が促進しにくい場合がある。When the aperture ratio is less than 60%, the flow velocity of water passing through the current plate 14 becomes excessive, and the impact force causes a phenomenon in which the flocs of the current plate 14 are damaged. Furthermore, the laminar flow state near the rectifying plate 14 may be disturbed, making it difficult to promote floc generation.
開口率８０％以上では、整流板１４の支持作用が弱くな
り充分なスラッジブランケット層３１を形成しにくくな
る。If the aperture ratio is 80% or more, the supporting effect of the current plate 14 becomes weak and it becomes difficult to form a sufficient sludge blanket layer 31.
整流板１４上方にはスラッジブランケット層３１のスラ
ッジを間欠的又は連続的に排出するスラッジ排出管３４
が配管される、３スラツジ排出管３４にはバルブ３６が
管路中に取り付けられている。Above the current plate 14 is a sludge discharge pipe 34 that discharges the sludge of the sludge blanket layer 31 intermittently or continuously.
A valve 36 is installed in the three-sludge discharge pipe 34 to which the sludge is piped.
更に、スラッジブランケット層３１の上方にはろ材層１
６が設けられている。ろ材層１６はスラッジブラケ７＋
−層を通過したｉ数細フロンクを最終的に捕捉する機能
を有する。ろ材層１６は空隙率８０〜９５％が望ましい
。空隙率が８０％以下の場合は、例えば粒状ろ材（砂、
アンスラサイト）の空隙率は約５０％であり、その分、
濁質の蓄積限界が低下する。また、９５％を越えると濁
質の捕捉作用が低下し、Ｓ’ｆＺがろ材をすり抜ける率
が増加する。Furthermore, a filter layer 1 is provided above the sludge blanket layer 31.
6 is provided. The filter layer 16 is a sludge bracket 7+
- It has the function of finally capturing the i-number fronks that have passed through the layer. The filter medium layer 16 preferably has a porosity of 80 to 95%. If the porosity is 80% or less, use granular filter media (sand,
The porosity of anthracite is approximately 50%, and
The accumulation limit of suspended solids is lowered. Moreover, when it exceeds 95%, the turbidity trapping effect decreases, and the rate at which S'fZ slips through the filter medium increases.
一方、ろ材の比重は１０以下が望ましい。この場合逆洗
時に洗浄水を下向流で流すと、容易にろ材が分散し、移
動するので、捕捉した粒子、フロックのろ材からの離脱
、剥離効果が良くなる。On the other hand, the specific gravity of the filter medium is preferably 10 or less. In this case, when the washing water is flowed downward during backwashing, the filter medium is easily dispersed and moved, so that the detachment and peeling effect of captured particles and flocs from the filter medium is improved.
ろ材の比重が１０以上の場合は逆洗の下向流でよ、ろ材
は相互に圧密されるだけで動かない。また、洗浄を上向
流で行ってもろ材を流動化させるには多量の洗浄水が必
要となる。ろ材層１６には洗浄水流人管３８及び洗浄排
水排出管４０が取付けられる。また、ろ材層１６を通過
した処理水を排出する排出管４２が接続されている。ス
ラッジ排出管３４と同様に洗浄水流人管３８、洗浄排水
排出管４０の管路中にはバルブ３７．３９がそれぞれ取
り付けられている。If the specific gravity of the filter media is 10 or more, use a downward flow of backwashing.The filter media will only be compressed together and will not move. Further, even if washing is performed in an upward flow, a large amount of washing water is required to fluidize the filter medium. A cleaning water flow pipe 38 and a cleaning waste water discharge pipe 40 are attached to the filter layer 16. Further, a discharge pipe 42 for discharging the treated water that has passed through the filter layer 16 is connected. Similar to the sludge discharge pipe 34, valves 37 and 39 are installed in the cleaning water flow pipe 38 and the cleaning waste water discharge pipe 40, respectively.
前記の如く構成した本発明に係る廃水の固液分能装置の
作用は以下の通りである。第１図に示すように、予めス
クリーン等により夾雑物が取り除かれた廃水が廃水導入
管２０を通って凝集［曹１０に導入される。凝集槽１０
において、凝集剤２４、必要に応じて凝集助剤２６を添
加する。そして、凝集槽ｌＯ内で廃水の攪拌を１１００
ｒｐ以上の高速で行い、充分に混合する。尚、凝集助剤
２６は凝集槽１０出口の供給管２８内に注入してもよい
。The operation of the wastewater solid-liquid separation apparatus according to the present invention constructed as described above is as follows. As shown in FIG. 1, wastewater from which impurities have been removed in advance by a screen or the like passes through a wastewater introduction pipe 20 and is introduced into a coagulation system 10. Coagulation tank 10
In this step, a flocculant 24 and, if necessary, a flocculating aid 26 are added. Then, the waste water was stirred in the flocculation tank 10 at 1100 °C.
Mix thoroughly at high speed (RP or higher). Note that the flocculation aid 26 may be injected into the supply pipe 28 at the outlet of the flocculation tank 10.
凝集槽１０を通過ｊ−た液は供給管２８を通って円筒型
固液分離槽１２内に接線方向に導入され、分＃槽１２内
で旋回流を生じながら上方へと移動する。この移動の際
にフロックは粗大化され、大きなフロックは沈降し固液
分離槽１２内下部のフロック沈降部に沈積する。沈積１
７たフロックは沈降汚泥排出管３３から間欠的或いは連
続的に排出される。一方、上方へ移動した液は整流板１
４によって整流され、旋回流を停止させる。整流板１４
によって旋回流が停止させられると、フロックの沈降が
促進されろ。整流板１４を通過した水はゆるやかな下向
流の安定したＮ流状性を形成［７、ここでもフロックの
形成が進行する。これは（１）整流板を自体のフロック
支持及び沈降阻止効果、（１１）整流板を通る水の流速
が開孔率に反比例して相対的に速くなることによる上向
水流による沈降阻止効果によるものである。この結果、
フロックが整流板上方に保持堆積し、スラッジブランケ
ット層３１が形成され、このプランケラ）９３１でのフ
ロック相互の結びつきによる粗大化が促進する。また、
下方から上向流で新たにこの層に流入する水の濁質やフ
ロックも、このブランケット層３１を通過する過程で捕
捉され易くなる。The liquid that has passed through the aggregation tank 10 is tangentially introduced into the cylindrical solid-liquid separation tank 12 through the supply pipe 28, and moves upward within the separation tank 12 while generating a swirling flow. During this movement, the flocs become coarse, and the large flocs settle and are deposited in the floc settling section in the lower part of the solid-liquid separation tank 12. Deposition 1
The 7 flocs are discharged from the settled sludge discharge pipe 33 intermittently or continuously. On the other hand, the liquid that moved upward is
4 to stop the swirling flow. Current plate 14
When the swirling flow is stopped, sedimentation of flocs will be promoted. The water that has passed through the current plate 14 forms a stable N flow shape with a gentle downward flow [7, where the formation of flocs also progresses. This is due to (1) the floc support and sedimentation prevention effect of the current plate itself, and (11) the sedimentation prevention effect due to the upward water flow due to the flow rate of water passing through the current plate becoming relatively faster in inverse proportion to the porosity. It is something. As a result,
The flocs are retained and deposited above the current plate, forming a sludge blanket layer 31, and coarsening due to mutual bonding of the flocs in the plancher 931 is promoted. Also,
The turbidity and flocs of water newly flowing into this layer in an upward flow from below are also easily captured during the process of passing through this blanket layer 31.
即ち、剪断力の低下によりフロキュレーンヨンが促進さ
れ粗大化したフロックを沈降させると共に、整流板１４
上方に弱い層流を起こしスラッジブランケント層３１を
形成する。また、整流板１４はスラッジブランケット層
３１が沈降しないよう支持する働きを有する。In other words, floccule formation is promoted by the decrease in shear force, and the coarse flocs are allowed to settle, and the current plate 14
A weak laminar flow is generated upward to form a sludge blanket layer 31. Further, the current plate 14 has a function of supporting the sludge blanket layer 31 so that it does not settle.
スラッジブランケット層３１は、スラッジの蓄積と共に
下方から上向流で新たに通過する濁質や微測なフロック
の一部を吸着分離する。スラッジブランケット層３１の
高さは１ｍ〜２ｍが適当であり、その高さを維持するた
めスラッジをスラッジ排出管３６から適宜排出する。The sludge blanket layer 31 adsorbs and separates part of the turbidity and minute flocs that newly pass through in an upward flow from below as sludge accumulates. The appropriate height of the sludge blanket layer 31 is 1 m to 2 m, and in order to maintain this height, the sludge is appropriately discharged from the sludge discharge pipe 36.
スラッジブランケット層３１を通過した液はろ材層１６
に導入される。整流板１４上方のブランケット層３１を
経た水中には、まだ、微細な粒子が残存している。従っ
て、この残存粒子を必要に応じて捕捉すべく、ろ材層１
６が存在する。ろ材層１６は粒状ろ材よりは、むしろ、
空隙率が大きく、比表面積の大きいものを選択する。即
ち、スクラバー等に用いる接触充填材などが好ましい。The liquid that has passed through the sludge blanket layer 31 is transferred to the filter medium layer 16
will be introduced in Fine particles still remain in the water that has passed through the blanket layer 31 above the current plate 14. Therefore, in order to capture these remaining particles as necessary, the filter medium layer 1
There are 6. Rather than granular filter media, the filter media layer 16 is
Select one with a large porosity and a large specific surface area. That is, contact fillers used in scrubbers and the like are preferred.
ろ材層においては、ろ材の存在により、流速が早い部分
と、流速が０に近い部分とが広い流速範囲で無数に分布
することになり、流速が遅い部分に沈積、付着した微細
粒子やフロックがしだいに成長して、ろ材の空隙部分に
停まり、この粗大化フロックが連鎖して、通過する微細
粒子やフロックを次々に捕捉する。ろ材層でのフロック
の蓄積量は限度があるので、はぼ飽和した時間Ｈ毎に逆
洗を繰返す。In the filter media layer, due to the presence of the filter media, there are numerous areas where the flow rate is high and areas where the flow rate is close to 0 are distributed over a wide flow rate range, and fine particles and flocs that are deposited and attached to the areas where the flow rate is slow are distributed. Gradually, they grow and stop in the voids of the filter medium, and these coarsened flocs form a chain and capture passing fine particles and flocs one after another. Since the amount of flocs accumulated in the filter media layer is limited, backwashing is repeated every time H when the filter is saturated.
前記のように構成した本発明に係る固液分離装置の性能
試験結果は以下のとおりである。廃水は、雨天時流入下
水を用い、良好な水質を得ることができた。また、固夜
分雅［ｇ１２のＬＶ（線速度）は３５ｍ／ｈであり、こ
の値から主要設置ｍの必要面偵を試算した結果、従来の
凝集沈殿処理装置、砂ろ過処理装置に比較して大幅な省
スペース化を図ることができることが確ｇ７Ｊされた。The performance test results of the solid-liquid separator according to the present invention configured as described above are as follows. As wastewater, we used sewage that flows in during rainy days, and we were able to obtain good water quality. In addition, the LV (linear velocity) of Goyobunya [g12] is 35 m/h, and as a result of calculating the required space for the main installation m from this value, it was found that the LV (linear velocity) of Goyabunkaya [g12 It has been confirmed that it is possible to achieve significant space savings.
以上説明したように本発明に係る廃水の固液分離装置に
よれば、円筒型固液分離槽に於いて、下部にフロー）り
沈降部を形成すると共に、廃水の流入口上方に整流板を
設け、整流板の上方にスラッジブランケット層を形成す
るようにしたので、廃水中の微細なフロックはスラッジ
ブランケットで除去される。これにより整流板上方のる
材層の目詰まり等が少なくなり、その保守も容易となる
。As explained above, according to the wastewater solid-liquid separator according to the present invention, in the cylindrical solid-liquid separation tank, a flow settling part is formed at the lower part, and a rectifying plate is provided above the wastewater inlet. Since a sludge blanket layer is formed above the current plate, fine flocs in wastewater are removed by the sludge blanket. This reduces clogging of the material layer above the current plate and facilitates its maintenance.
また、従来の固液分離装置に比較して廃水の処理速度が
向上しているので、処理場の単位面積当りの処理能力が
向上し、処理場の省スペース化、コンパクト化が可能と
なる。Furthermore, since the processing speed of wastewater is improved compared to conventional solid-liquid separators, the processing capacity per unit area of the treatment plant is improved, making it possible to save space and make the treatment plant more compact.
第１図は本発明に係る固液分離装置の用略を示す系統図
、第２図は円筒型固液分離槽の内部構造を示す断面図、
第３図は整流板の構造を示す斜視図、第４図は従来の廃
水の固液分離装置を示す正面図である。
１０・凝集隋、 １２・・・円筒型固液分離槽、１４
・・・整流板、 １６・・ろ材種、 ２４・・・凝集
剤、２６−・・凝集助剤、 ３１・・・スラッジブラ
ンケット層。
第
面FIG. 1 is a system diagram showing the use of the solid-liquid separation device according to the present invention, and FIG. 2 is a sectional view showing the internal structure of a cylindrical solid-liquid separation tank.
FIG. 3 is a perspective view showing the structure of a rectifying plate, and FIG. 4 is a front view showing a conventional solid-liquid separation device for wastewater. 10. Coagulation, 12... Cylindrical solid-liquid separation tank, 14
... Straightening plate, 16... Filter medium type, 24... Coagulant, 26-... Coagulation aid, 31... Sludge blanket layer. Front page
Claims (2)
中間位置に旋回上向流で流入させ、前記円筒型固液分離
槽の下部にフロック沈降部を形成すると共に前記廃水の
流入口上方に固液分離槽の横断方向に整流板を配置した
ことを特徴とする廃水の固液分離装置。(1) Wastewater mixed with a flocculant is caused to flow into the middle of a cylindrical solid-liquid separation tank in a swirling upward flow, and a floc settling part is formed in the lower part of the cylindrical solid-liquid separation tank, and the wastewater flows A solid-liquid separation device for wastewater, characterized in that a rectifying plate is arranged in a transverse direction of a solid-liquid separation tank above an inlet.
ろ材層を設けたことを特徴とする請求項（１）の廃水の
固液分離装置。(2) The solid-liquid separation device for wastewater according to claim 1, characterized in that the cylindrical solid-liquid separation tank is provided with a filter layer above the current plate.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11006689A JPH02284604A (en) | 1989-04-27 | 1989-04-27 | Solid-liquid separation for waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11006689A JPH02284604A (en) | 1989-04-27 | 1989-04-27 | Solid-liquid separation for waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH02284604A true JPH02284604A (en) | 1990-11-22 |
| JPH0560966B2 JPH0560966B2 (en) | 1993-09-03 |
Family
ID=14526198
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11006689A Granted JPH02284604A (en) | 1989-04-27 | 1989-04-27 | Solid-liquid separation for waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH02284604A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6290842B1 (en) * | 1998-05-08 | 2001-09-18 | Organo Corporation | Coagulator |
-
1989
- 1989-04-27 JP JP11006689A patent/JPH02284604A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US6290842B1 (en) * | 1998-05-08 | 2001-09-18 | Organo Corporation | Coagulator |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0560966B2 (en) | 1993-09-03 |
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