JPH03296494A - Treatment apparatus for organic polluted water - Google Patents
Treatment apparatus for organic polluted waterInfo
- Publication number
- JPH03296494A JPH03296494A JP2097622A JP9762290A JPH03296494A JP H03296494 A JPH03296494 A JP H03296494A JP 2097622 A JP2097622 A JP 2097622A JP 9762290 A JP9762290 A JP 9762290A JP H03296494 A JPH03296494 A JP H03296494A
- Authority
- JP
- Japan
- Prior art keywords
- tank
- flow rate
- sedimentation separation
- filter bed
- 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
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 title claims description 69
- 238000004062 sedimentation Methods 0.000 claims abstract description 46
- 238000000926 separation method Methods 0.000 claims abstract description 39
- 238000012935 Averaging Methods 0.000 claims abstract description 34
- 239000002351 wastewater Substances 0.000 claims abstract description 31
- 238000007654 immersion Methods 0.000 claims abstract description 18
- 239000010865 sewage Substances 0.000 claims abstract description 13
- 239000010802 sludge Substances 0.000 claims abstract description 13
- 238000005273 aeration Methods 0.000 claims abstract description 7
- 238000005406 washing Methods 0.000 claims description 21
- 238000004140 cleaning Methods 0.000 claims description 18
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 6
- 229910052760 oxygen Inorganic materials 0.000 claims description 6
- 239000001301 oxygen Substances 0.000 claims description 6
- 239000007789 gas Substances 0.000 claims description 5
- 239000000126 substance Substances 0.000 claims 1
- 239000007788 liquid Substances 0.000 abstract description 7
- 241000894006 Bacteria Species 0.000 abstract 1
- 238000005276 aerator Methods 0.000 abstract 1
- 230000001174 ascending effect Effects 0.000 abstract 1
- 230000000644 propagated effect Effects 0.000 abstract 1
- 230000001902 propagating effect Effects 0.000 abstract 1
- 244000005700 microbiome Species 0.000 description 9
- 238000003860 storage Methods 0.000 description 9
- 230000000694 effects Effects 0.000 description 8
- 239000002245 particle Substances 0.000 description 7
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 6
- 238000001914 filtration Methods 0.000 description 5
- 239000008187 granular material Substances 0.000 description 5
- 230000005484 gravity Effects 0.000 description 4
- 239000000463 material Substances 0.000 description 4
- 238000000034 method Methods 0.000 description 4
- RHZUVFJBSILHOK-UHFFFAOYSA-N anthracen-1-ylmethanolate Chemical compound C1=CC=C2C=C3C(C[O-])=CC=CC3=CC2=C1 RHZUVFJBSILHOK-UHFFFAOYSA-N 0.000 description 3
- 239000003830 anthracite Substances 0.000 description 3
- 238000004519 manufacturing process Methods 0.000 description 3
- 230000000813 microbial effect Effects 0.000 description 3
- 238000002347 injection Methods 0.000 description 2
- 239000007924 injection Substances 0.000 description 2
- 238000006243 chemical reaction Methods 0.000 description 1
- 239000000084 colloidal system Substances 0.000 description 1
- 238000010276 construction Methods 0.000 description 1
- 238000009792 diffusion process Methods 0.000 description 1
- HNPSIPDUKPIQMN-UHFFFAOYSA-N dioxosilane;oxo(oxoalumanyloxy)alumane Chemical compound O=[Si]=O.O=[Al]O[Al]=O HNPSIPDUKPIQMN-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 238000005516 engineering process Methods 0.000 description 1
- 238000007667 floating Methods 0.000 description 1
- 238000009408 flooring Methods 0.000 description 1
- 239000010800 human waste Substances 0.000 description 1
- 239000010842 industrial wastewater Substances 0.000 description 1
- 229910052500 inorganic mineral Inorganic materials 0.000 description 1
- 238000009434 installation Methods 0.000 description 1
- 239000011707 mineral Substances 0.000 description 1
- 239000002367 phosphate rock Substances 0.000 description 1
- 238000001556 precipitation Methods 0.000 description 1
- 239000008262 pumice Substances 0.000 description 1
- 230000029058 respiratory gaseous exchange Effects 0.000 description 1
- 239000004575 stone Substances 0.000 description 1
- 230000002123 temporal effect Effects 0.000 description 1
- 210000003437 trachea Anatomy 0.000 description 1
Classifications
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Abstract
Description
【発明の詳細な説明】
〔産業上の利用分野〕
本発明は、下水、各種産業廃水、し尿、浄化槽汚泥など
種々の有機性汚水を浄化処理する新規処理装置に関する
ものである。DETAILED DESCRIPTION OF THE INVENTION [Field of Industrial Application] The present invention relates to a new treatment device for purifying various organic wastewaters such as sewage, various industrial wastewaters, human waste, and septic tank sludge.
従来より、好気性浸漬濾床装置は公知である。 Aerobic submerged filter bed devices are known in the art.
この従来の装置は、第２図に示すように、槽３１の水面
下に、アンスラサイト、粒状活性炭、各種粒状鉱物、ブ
ラスチンク粒子など任意の粒状濾材の充填層（浸漬濾床
３２と呼ぶ）を設け、該浸漬濾床３２内下部に空気等の
酸素含有ガスの散気管３３を配備したものである。また
、このような好気性浸漬濾床装置には、沈殿池３４．処
理水貯槽３８、洗浄排水貯槽４０が付設されている。As shown in FIG. 2, this conventional device has a packed bed (referred to as an immersion filter bed 32) of any granular filter material such as anthracite, granular activated carbon, various granular minerals, and brassink particles under the water surface of a tank 31. A diffuser pipe 33 for oxygen-containing gas such as air is provided in the lower part of the submerged filter bed 32. Further, such an aerobic immersion filter device includes a settling tank 34. A treated water storage tank 38 and a washing wastewater storage tank 40 are attached.
しかして、有機性汚水（原水）は、沈殿池３４から原水
流入管３５を経て槽３１内に流入し、浸漬濾床３２を下
向流または上向流（第２図は下向流の場合）で流遇し、
粒状濾材表面の微生物及びブロワ−３６から散気管３３
を経て散気される酸素含有ガスの気泡と接触し、ＢＯＤ
が除去されると共に、原水ＳＳも濾過除去され、処理水
となって処理水流出管３７を経て処理水貯槽３８に至る
。このような処理を継続するにつれ、浸漬濾床３２内に
捕捉されたＳＳと微生物量の増加によって、濾過抵抗が
増加して処理を続けることが困難になるので、処理水貯
槽３８内に貯留されている清澄な処理水をポンプ３９に
よって浸漬濾床３２の下部に供給し、浸漬濾床３２を洗
浄する。Organic sewage (raw water) flows from the settling tank 34 into the tank 31 through the raw water inflow pipe 35, and flows through the submerged filter bed 32 in a downward or upward flow (Fig. 2 shows the case of downward flow). ),
Microorganisms on the surface of the granular filter medium and the air diffuser 33 from the blower 36
contact with bubbles of oxygen-containing gas diffused through
At the same time, the raw water SS is also filtered out and becomes treated water, which reaches the treated water storage tank 38 via the treated water outflow pipe 37. As such treatment continues, the amount of SS and microorganisms trapped in the immersed filter bed 32 increases, increasing the filtration resistance and making it difficult to continue the treatment, so the treated water is stored in the treated water storage tank 38. Clear treated water is supplied to the lower part of the submerged filter bed 32 by a pump 39 to wash the submerged filter bed 32.
浸漬濾床３２の洗浄排水は、槽３１の上部から洗浄排水
貯槽４０に至り、この洗浄排水はポンプ４１で沈殿池３
４に供給されてＳＳが沈降分離され、原水と洗浄排水流
量との合計量が再び浸漬濾床３２へ供給される。The washing wastewater from the immersion filter bed 32 reaches the washing wastewater storage tank 40 from the upper part of the tank 31, and this washing wastewater is sent to the settling tank 3 by a pump 41.
4, the SS is sedimented and separated, and the total amount of raw water and washing wastewater flow rate is again supplied to the submerged filter bed 32.
しかしながら、第２図の従来装置には次のような大きな
欠点があり、さらに優れた装置及びシステム構成が切望
されている。However, the conventional device shown in FIG. 2 has the following major drawbacks, and an even better device and system configuration are desperately needed.
■ 原水ＳＳが多い場合、第２図のように好気性浸漬濾
床装置の前段に沈殿池を設け、ＳＳの大部分を除去しな
ければならない。さもないと、好気性浸漬濾床装置の炉
床部で速やかに目づまり（閉塞）が進行し、好気性浸漬
濾床装置の運転が不可能となり、炉床洗浄頻度も激増す
る。しかも、沈殿池の沈降分離速度はせいぜい３０ｍ／
日程度しか採れないので、沈殿池の建設費。■ If there is a lot of SS in the raw water, it is necessary to install a settling tank in front of the aerobic immersion filter as shown in Figure 2 to remove most of the SS. Otherwise, the hearth of the aerobic immersed filter will rapidly become clogged (occlusion), making it impossible to operate the aerobic immersed filter, and the frequency of hearth cleaning will increase dramatically. Moreover, the sedimentation separation speed of the sedimentation tank is at most 30 m/
Since the amount of water that can be collected is only about a day, the cost of constructing a sedimentation pond is high.
設置スペースが大きくなる。Installation space becomes larger.
■ 炉床の洗浄時に炉床容積の２．５倍という多量の洗
浄用水が必要で、洗浄用水として第２図のように好気性
浸漬濾床装置の処理水を多量に使わなければならない、
従って、処理水生産効率が低く、しかも大容量の処理水
貯槽が必要となる。■ When cleaning the hearth, a large amount of cleaning water is required, which is 2.5 times the volume of the hearth, and a large amount of treated water from the aerobic immersion filter device must be used as the cleaning water, as shown in Figure 2.
Therefore, the production efficiency of treated water is low, and a large capacity treated water storage tank is required.
■ 炉床の洗浄排水を、第２図のように前段の沈殿池に
流入させて処分しているため、好気性浸漬濾床装置には
原水と洗浄排水の合計流量が流入することになる。この
結果、好気性浸漬濾床装置への水量負荷が増加し、好気
性浸漬濾床装置の直径を大きくしなければならなくなっ
ている。（洗浄頻度が多くなるほど好気性浸漬濾床装置
の水量負荷は激増する）
本発明の課題は従来装置の前記■〜■の欠点を完全に解
決し、有機性汚水のＳＳ除去とＢＯＤ除去をきわめて効
果的に達成できるとともに、好気性浸漬濾床の洗浄排水
の処理と洗浄用水の生産とを、同一の好気性浸漬濾床装
置を利用して行える画期的処理装置を提供することであ
る。■ Since the washing wastewater from the hearth is disposed of by flowing into the sedimentation tank in the previous stage as shown in Figure 2, the total flow of raw water and washing wastewater flows into the aerobic submerged filter device. As a result, the water load on the aerobic submerged filter bed device increases, making it necessary to increase the diameter of the aerobic submerged filter bed device. (The more frequently the cleaning frequency increases, the more the water load on the aerobic immersion filter device increases dramatically.) The object of the present invention is to completely solve the above-mentioned drawbacks of conventional devices, and to completely remove SS and BOD from organic wastewater. It is an object of the present invention to provide an epoch-making treatment device which can effectively achieve the above-mentioned results and which can process wastewater from washing an aerobic immersed filter bed and produce washing water using the same aerobic immersion filter bed device.
本発明は、原水流入部と流出部を備え槽内に曝気装置を
配備した流量平均化槽と、槽内上方部に粒状濾材を充填
した浸漬濾床を保持すると共に該浸漬濾床の内部又は下
部に酸素含有ガスの散気装置を配備し、槽内下方部を沈
降分離部とし、前記浸漬濾床より上方に処理水流出部と
洗浄排水流出部を設けた処理槽とからなり、前記流量平
均化槽の流出部を前記処理槽の沈降分離部に連結し、さ
らに前記処理槽の洗浄排水流出部を沈降分離部に連結し
たことを特徴とする有機性汚水の処理装置であり、さら
に、前記処理槽の洗浄排水流出部を前記流量平均化槽を
介して沈降分離部に連結したこと、及び前記処理槽の沈
降分離部に沈降した汚泥の一部を前記流量平均化槽に供
給する流路を設けたことをも特徴とするものである。The present invention provides a flow rate averaging tank having a raw water inlet and an outlet and an aeration device installed inside the tank, and an immersed filter bed filled with granular filter media in the upper part of the tank, and an internal or It consists of a treatment tank equipped with an oxygen-containing gas diffuser in the lower part, a sedimentation separation part in the lower part of the tank, and a treated water outflow part and a washing wastewater outflow part above the immersion filter bed, and the flow rate is as follows. An organic sewage treatment apparatus characterized in that an outflow part of the averaging tank is connected to a sedimentation separation part of the treatment tank, and further, a washing wastewater outflow part of the treatment tank is connected to the sedimentation separation part, and further, The cleaning wastewater outflow part of the treatment tank is connected to the sedimentation separation part via the flow rate averaging tank, and a flow supplying a part of the sludge settled in the sedimentation separation part of the treatment tank to the flow rate averaging tank. It is also characterized by the provision of a road.
第１図のように構成された本発明装置の流量平均化槽１
に、ＳＳ、溶解性ＢＯＤ等を含む有機性汚水（原水）を
流入させ、時間的に変動する原水流量を平均化する。従
って、流量平均化［１内の水位は流入量の時間変動に伴
って上下動する。Flow rate averaging tank 1 of the device of the present invention configured as shown in FIG.
Organic wastewater (raw water) containing SS, soluble BOD, etc. is introduced into the tank, and the temporally varying flow rate of the raw water is averaged. Therefore, the water level within flow rate averaging [1] moves up and down with time fluctuations in the inflow amount.
このように、流量平均化槽ｌで原水流入量の時間的変動
を平均化する間に曝気装置により曝気を受は増殖する微
生物によって水中の溶解性ＢＯＤの一部が除去される。In this way, while the temporal fluctuations in the inflow of raw water are averaged in the flow rate averaging tank 1, part of the soluble BOD in the water is removed by the microorganisms that are aerated by the aeration device and proliferate.
流量平均化槽１内には微生物量を高濃度に維持すること
が好ましく、微生物付着担体６を装填するとよく、特に
微生物付着担体６として比重１．０以下の粒状濾材は、
槽内の水位に上下動に伴って上下する充填層を維持でき
るから、最も好適である。It is preferable to maintain the amount of microorganisms at a high concentration in the flow rate averaging tank 1, and a microorganism-adhering carrier 6 is preferably loaded, and in particular, a granular filter medium with a specific gravity of 1.0 or less is used as the microorganism-adhering carrier 6.
This is most suitable because it is possible to maintain a packed bed that rises and falls as the water level in the tank moves up and down.
このようにして、原水の流入量の変動が平均化され、同
時に微生物によってＢＯＤ等の一部が除去された原水は
、処理槽１１内の沈降分離部１４に供給され、原水中の
ＳＳと流量平均化槽１で増殖した活性汚泥ＳＳが沈降分
離される。In this way, fluctuations in the inflow amount of raw water are averaged, and at the same time, the raw water from which a part of BOD etc. has been removed by microorganisms is supplied to the sedimentation separation section 14 in the treatment tank 11, and the SS in the raw water and the flow rate are The activated sludge SS grown in the averaging tank 1 is sedimented and separated.
沈降分離部１４においてＳＳの大部分が沈降除去された
液は、上向流となって沈降分離部１４の上部の水面下に
設けられた浸漬濾床１２内に流入してゆき、沈降しなか
った微細ＳＳが濾過除去されると共に、浸漬濾床１２を
構成する粒状濾材表面に生物膜と粒状が材間に空隙に保
持された微生物フロックとの両者によって、溶解性ＢＯ
Ｄが効果的に除去され、ＮＦＩ３−Ｎも硝化される。即
ち、浸漬濾床１２においては、生物処理とＳＳのが過が
同時に行われ、生物の呼吸に必要な酸素は散気管１３か
ら散気されて浸漬濾床１２内を上昇する気泡によって供
給される。The liquid from which most of the SS has been sedimented and removed in the sedimentation separation section 14 flows upward into the submerged filter bed 12 provided below the water surface above the sedimentation separation section 14, and does not settle. At the same time, the soluble BO is removed by filtration, and the biofilm on the surface of the granular filter media constituting the immersed filter bed 12 and the microbial flocs in which particles are held in the spaces between the media are removed.
D is effectively removed and NFI3-N is also nitrified. That is, in the submerged filter bed 12, biological treatment and SS filtration are performed simultaneously, and the oxygen necessary for respiration of living organisms is supplied by air bubbles that are diffused from the aeration pipe 13 and rise within the submerged filter bed 12. .
このような構成によって、処理槽１１においてＳＳの沈
降、ｔｐ遇、 ＲＯＤ除去、 Ｍ２Ｓ−Ｎの硝化がきわ
めて効果的に進行し、処理槽１１の水面から、５Ｓ１０
■／ｊ、 ＢＯＤ １０■／！以下の清澄な処理水が泉
のように湧出し、処理水流出管１９から流出する。With such a configuration, sedimentation of SS, TP treatment, ROD removal, and nitrification of M2S-N proceed extremely effectively in the treatment tank 11, and 5S10 from the water surface of the treatment tank 11 is
■/j, BOD 10■/! The following clear treated water gushes out like a spring and flows out from the treated water outflow pipe 19.
特に本発明では、流量平均化槽１において原水中の溶解
性ＢＯＤの大部分を除去することができるので、浸漬濾
床１２へのＢＯＤ負荷を大幅に軽減し、生物の増殖に伴
う浸漬濾床１２の目づまり進行度が著しく緩慢になると
いう大きな効果がある。In particular, in the present invention, since most of the soluble BOD in the raw water can be removed in the flow rate averaging tank 1, the BOD load on the immersed filter bed 12 can be significantly reduced, and the immersed filter bed can be This has the great effect of significantly slowing down the progress of clogging.
さらに、流量平均化槽１において、原水中のＳＳが活性
汚泥と接触して吸着され、粒径増加現象を起こすので、
処理槽１１の沈降分離部１４における沈降性が向上する
。この結果、浸漬濾床１２に流入するＳＳ量が減少し、
浸漬濾床１２の濾過抵抗の増加も著しく少な（なるとい
う効果がある。Furthermore, in the flow rate averaging tank 1, SS in the raw water comes into contact with activated sludge and is adsorbed, causing a particle size increase phenomenon.
The sedimentation property in the sedimentation separation section 14 of the treatment tank 11 is improved. As a result, the amount of SS flowing into the immersion filter bed 12 is reduced,
The increase in filtration resistance of the immersed filter bed 12 is also significantly reduced.
しかして、浸漬濾床１２における処理を長時間（５〜１
０日程度）継続すると、浸漬濾床１２におけるＳＳ捕捉
量が過剰になり、ショートパスを招きやすくなるので、
浸漬濾床１２の洗浄を行う。Therefore, the treatment in the immersion filter bed 12 is carried out for a long time (5 to 1
If it continues (about 0 days), the amount of SS captured in the immersion filter bed 12 will become excessive, which will easily lead to short passes.
The immersion filter bed 12 is cleaned.
浸漬濾床１２の洗浄方法は、次のような本発明独自の方
法が好適である。As a method for cleaning the submerged filter bed 12, the following method unique to the present invention is suitable.
じ、洗浄排水流出管２１の弁２０ を開放する。Similarly, the valve 20 of the cleaning drainage outflow pipe 21 to open.
に増加し、浸漬濾床１２内に強い 気液混相撹乱流を発生させ、流量 平均化槽１から流入する液の上昇 流によってＳＳを洗い出し、その洗 浄排水を沈降分離部１４に導く。increases in strength within the immersed filter bed 12. Generates a gas-liquid multiphase turbulent flow and increases the flow rate. Rise of liquid flowing from averaging tank 1 The SS is washed out by the flow, and the washing is carried out. The purified waste water is guided to the sedimentation separation section 14.
洗浄排水を沈降分離部１４に導く には、直接沈降分離部１４に導く ことができるが、第１図示例のよ うに、洗浄排水流出管２１から流 量平均化槽１内に流入させたのち 沈降分離部１４へ導くことが好ま しい（この場合、沈降分離部１４ への水量を定常処理時より増加さ せるとよい）、このような操作を 所定時間行う。Guide the cleaning wastewater to the sedimentation separation section 14 In this case, it is directly led to the sedimentation separation section 14. However, as shown in the first example, water from the cleaning wastewater outflow pipe 21. After flowing into the volume averaging tank 1 It is preferable to introduce it to the sedimentation separation section 14. (in this case, sedimentation separation section 14 The amount of water is increased from that during steady processing. ), perform operations like this Do this for a specified period of time.
した時点で、散気管１３からの散 気量を定常運転時に減少し、洗浄 排水流出管２１の弁２０を閉じ、 処理水流出管１９の弁１８を開放 する。At that point, the air diffuser from the air diffuser 13 is Reduces air volume during steady operation and cleans Close the valve 20 of the wastewater outflow pipe 21, Open the valve 18 of the treated water outflow pipe 19 do.
築
このように、本発明においては、従来装置（例えば第２
図参照）において不可欠となっていた浸＊Ｆ床工２の処
理水を消費する洗浄を行わなくてよいという、重要な効
果がある。この結果、処理水生産効率を、従来装置より
大幅に向上させることができる。As described above, in the present invention, the conventional device (for example, the second
This has the important effect of eliminating the need for cleaning that consumes the treated water of the immersion *F flooring 2, which was indispensable in the previous method (see figure). As a result, the efficiency of producing treated water can be significantly improved compared to conventional devices.
しかも、本発明においては、浸漬濾床１２に流入する液
のＢＯＤ、 ＳＳが、流量平均化槽１における生物処理
機能及び沈降分離部１４における沈降分離機能によって
減少しているために、洗浄操作終了時の浸漬濾床１２内
に滞留している液はかなり清澄な水質となっている。こ
の結果、洗浄終了後の処理水は、容易にかつ速やかに良
好な水質に復帰する。Moreover, in the present invention, since the BOD and SS of the liquid flowing into the submerged filter bed 12 are reduced by the biological treatment function in the flow rate averaging tank 1 and the sedimentation separation function in the sedimentation separation section 14, the cleaning operation is completed. The liquid remaining in the immersion filter bed 12 at this time has a fairly clear water quality. As a result, the treated water after cleaning is easily and quickly restored to good water quality.
さらに、本発明の他の好適実施態様を述べれば次の通り
である。Furthermore, other preferred embodiments of the present invention are as follows.
■ 処理槽１１の沈降分離部１４から排泥される汚泥の
一部を流量平均化槽１にリサイクルすると、流量平均化
槽ｌにおける８０１）除去効果を一層促進することがで
きる。(2) If a part of the sludge discharged from the settling section 14 of the treatment tank 11 is recycled to the flow rate averaging tank 1, the removal effect of 801) in the flow rate averaging tank 1 can be further promoted.
■ 処理槽１１の沈降分離部１４に供給される液に凝集
剤を注入することによって、ＳＳの沈降性向上、Ｐｏｔ
”−、ＣＯＤの除去率向上をはかることも好適である。■ By injecting a flocculant into the liquid supplied to the sedimentation separation section 14 of the treatment tank 11, the sedimentation properties of SS can be improved and the Pot
”-, it is also suitable to aim at improving the removal rate of COD.
■ 流量平均化槽１内で間欠曝気を行うことによって、
硝化脱窒、ＢＥ物脱リン作用を進行させることができる
。■ By performing intermittent aeration in the flow rate averaging tank 1,
Nitrification denitrification and BE matter dephosphorization can proceed.
本発明の一実施例を第１図を参照しつつ説明すれば、１
は流量平均化槽であって、原水流入管２が開口し、流出
管３が連結されている０才た、流量平均化槽１白下部に
は曝気装置、例えばプロワ−４に連なる空気の散気管５
が配備され、水中に好気性微生物を増殖させるものであ
るが、微生物量を高濃度に維持するには、微生物付着担
体６を槽内に装填しておくことが好ましい。An embodiment of the present invention will be described with reference to FIG.
is a flow rate averaging tank, in which the raw water inflow pipe 2 is open and the outflow pipe 3 is connected.At the lower part of the flow rate averaging tank 1 is an aeration device, for example, an air diffuser connected to a blower 4. Trachea 5
is provided to grow aerobic microorganisms in the water, but in order to maintain the amount of microorganisms at a high concentration, it is preferable to load a microorganism-attached carrier 6 into the tank.
微生物付着担体６としては、アンスラサイトシャモット
、抗火石１粒状活性炭、スポンジ粒状物１粒状プラスチ
ック、粒状発泡プラスチック。The microorganism adhesion carrier 6 includes anthracite chamotte, anti-fire stone, one granular activated carbon, one sponge granule, one granular plastic, and granular foamed plastic.
粒状軽量骨材などの各種粒状が材を使用することが、微
生物付着面積が大きく、エアレージ５ン効率を高めるこ
とができるために理想的であり、特に比重１．０以下の
浮上性粒状が材は、槽内水位の上下動に伴って上下する
充填層を維持できるので最も好適である。It is ideal to use various types of granular materials such as granular lightweight aggregates because they have a large area of microbial adhesion and can increase airage efficiency. Particularly, buoyant granules with a specific gravity of 1.0 or less are ideal. is most suitable because it can maintain a packed bed that moves up and down as the water level in the tank rises and falls.
一方、１１は処理槽であって、槽内の上方部には、アン
スラサイト、粒状活性炭９粒状軽量骨材スポンジ粒状物
１粒状プラスチック、発泡粒状プラスチック、粒状軽石
７粒状リン鉱石、ゼオライト粒子などの任意の粒状が材
を充填した浸漬濾床１２が設けられており、比重が１．
０以上の沈降性粒状が材を使用するときは、浸漬濾床１
２の下部を多孔性の支持部材ｌＯで支持し、比重１．０
未満の浮上性粒状が材を使用するときは、浸漬濾床１２
の上部に浮上性粒状が材の流出を阻止するネットなどの
多孔遣水部材１０′を設ける。なお、多孔通水部材１０
’は、必要により浸漬濾床１２の上下部に設けてもよい
、また、浸漬ｒ床１２の内部又は下部にはブロワ−１６
に連なる空気その他の酸素含有ガスを散気する散気管１
３が配備されている。On the other hand, 11 is a treatment tank, and the upper part of the tank contains anthracite, granular activated carbon, 9 granules, lightweight aggregate, 1 granular sponge, 1 granular plastic, foamed granular plastic, granular pumice, 7 granular phosphate rock, zeolite particles, etc. An immersed filter bed 12 filled with arbitrary granular material is provided, and the specific gravity is 1.
When using material with 0 or more sedimentary particles, submerged filter bed 1
The lower part of 2 is supported by a porous support member lO, and the specific gravity is 1.0.
When using material with less than 12 buoyant particles, the submerged filter bed 12
A porous water discharging member 10', such as a net, is provided on the upper part of the pipe to prevent floating particles from flowing out. Note that the porous water passing member 10
' may be provided at the upper and lower parts of the submerged filter bed 12 if necessary.
Diffusion pipe 1 that diffuses air and other oxygen-containing gas connected to
3 are deployed.
処理槽１１内の下方部は沈降分離部１４であり、排泥管
１５が連結され、また浸漬濾床１２より上方には、越流
ロンダー１７が設けられ、弁１８を備えた処理水流出管
１９と、弁２０を備えた洗浄排水流出管２１が連結され
ている。The lower part of the treatment tank 11 is a sedimentation separation part 14 to which a sludge removal pipe 15 is connected, and an overflow launder 17 is provided above the immersion filter bed 12, and a treated water outflow pipe equipped with a valve 18. 19 and a washing waste water outflow pipe 21 equipped with a valve 20 are connected.
また、流量平均化槽１の流出管３は、ポンプ２２を介し
て処理槽１１の沈降分離部１４に延長されて開口され、
その途中には凝集割注入管２３が接続されている。Further, the outflow pipe 3 of the flow rate averaging tank 1 is extended and opened to the sedimentation separation section 14 of the processing tank 11 via the pump 22,
An agglomerate injection pipe 23 is connected in the middle thereof.
前記処理槽１１の洗浄排水流出管２１は、沈降分離部１
４に連結されており、この洗浄排水流出管２１をそのま
ま沈降分離部１４に連結することができるが、第１図示
例のように、洗浄排水流出管２１を一旦流量平均化槽１
内に開口し、洗浄排水を流量平均化槽重を介して流出管
３から処理槽１１の沈降分離部１４に導くようにするこ
とも好ましい。The cleaning wastewater outflow pipe 21 of the processing tank 11 is connected to the sedimentation separation section 1
4, and the washing wastewater outflow pipe 21 can be directly connected to the sedimentation separation section 14, but as shown in the first example, the washing wastewater outflow pipe 21 is once connected to the flow rate averaging tank 1.
It is also preferable to open inward and guide the cleaning wastewater from the outflow pipe 3 to the sedimentation separation section 14 of the treatment tank 11 via a flow rate equalizing tank weight.
なお、洗浄排水は、別に設けた貯槽（図示せず）に−旦
貯留してから、流量平均化槽１に導くようにしたり、あ
るいは直接沈殿分離部１４に導くようにするのもよい。Note that the washing wastewater may be first stored in a separately provided storage tank (not shown) and then guided to the flow rate averaging tank 1 or directly to the precipitation separation section 14.
さらに、処理槽１１の排泥管１５から汚泥供給管２４を
分岐して流量平均化槽１に連結し、沈降分離部１４から
排泥される汚泥の一部を流量平均化槽１に供給すること
も好ましい態様である。Further, a sludge supply pipe 24 is branched from the sludge drain pipe 15 of the treatment tank 11 and connected to the flow rate averaging tank 1, and a part of the sludge discharged from the sedimentation separation section 14 is supplied to the flow rate averaging tank 1. This is also a preferred embodiment.
以上述べたように、本発明によれば、次のような多くの
重要効果を奏することができる。As described above, according to the present invention, the following many important effects can be achieved.
■ 単一の処理槽内で、ＳＳの沈降分離、 ＳＳの濾過
。■ Sedimentation separation of SS and filtration of SS in a single treatment tank.
ＢＯＤの生物学的除去、 ＮＨ３−Ｎの硝化という高度
の機能を進行させることができる。この結果、従来装置
では不可欠であった浸漬濾床とは別個の沈殿槽が不要に
なり、大幅な建設費の削減が可能になる。Advanced functions such as biological removal of BOD and nitrification of NH3-N can proceed. As a result, a sedimentation tank separate from the immersion filter bed, which was essential in conventional equipment, is no longer necessary, making it possible to significantly reduce construction costs.
■ 前段の流量平均化槽において、流量の平均化と同時
に、ＢＯＤの大半を餘去するとかできるので、浸漬濾床
のＢＯＤ負荷がきわめて小さくなってＮＨ３−Ｎの硝化
反応も進行しやすくなり、同時に浸漬濾床のが抗上昇が
著しく少なくなる。■ In the flow rate averaging tank at the front stage, most of the BOD can be removed at the same time as the flow rate is averaged, so the BOD load on the submerged filter bed becomes extremely small and the NH3-N nitrification reaction progresses more easily. At the same time, the resistance to rise of the submerged filter bed is significantly reduced.
■ 原水中の微細コロイドが、流量平均化槽内の微生物
フロックないし生物膜に吸着し、粒径が増加するので、
沈降分離部におけるＳＳの沈降分離効果が著しく向上す
る。■ Fine colloids in the raw water are adsorbed to microbial flocs or biofilms in the flow rate averaging tank, and the particle size increases.
The sedimentation separation effect of SS in the sedimentation separation section is significantly improved.
■ 浸漬濾床の洗浄に、従来装置のような処理水を消費
する水洗浄を行う必要がな（、洗浄排水それ自体を浸漬
濾床の洗浄用水として再利用することもでき、処理水生
産効率が非常に高い。■ It is not necessary to wash the immersed filter bed, which consumes treated water as in conventional equipment (the washing wastewater itself can be reused as water for washing the immersed filter bed, improving the production efficiency of treated water). is very high.
また、前段の流量平均化槽におけるＢＯＤ除去効果及び
沈降分離部でのＳＳの沈降分離効果により、浸漬濾床の
洗浄頻度も従来装置の１１５〜１／１０に減少される。Furthermore, due to the BOD removal effect in the flow rate averaging tank at the front stage and the sedimentation separation effect of SS in the sedimentation separation section, the cleaning frequency of the submerged filter bed is reduced to 115 to 1/10 of that of the conventional device.
■ 処理槽の水面から透視度の高いきわめて清澄な処理
水が泉のように湧出するので、美観が優れており、また
処理槽の水面から悪臭が発散することがない。■ Extremely clear treated water with high transparency gushes out like a spring from the water surface of the treatment tank, giving it a beautiful appearance and no bad odor emanating from the water surface of the treatment tank.
第１図は本発明の一実施例を示す縦断面図、第２図は従
来例を示す縦断面図である。
■・・・流量平均化槽、２・・・原水流入管、３・・・
流出管、４．１６．３６・・・ブロワ−１５，１３，３
３・・・散気管、６・・・微生物付着担体、１０・・・
支持材、１０’・・・多孔通水部材、１１・・・処理槽
、１２．３２・・・浸漬濾床、１４・・・沈降分離部、
１５・・・排泥管、１７・・・越流ロンダー１８．２０
・・・弁、１９．３７・・・処理水流出管、２１・・・
洗浄排水流出管、２２，３９．４１・・・ポンプ、２３
・・・凝集剤注入管、２４・・・汚泥供給管、３１・・
・槽、３４・・・沈殿池、３５・・・原水流入管、３８
・・・処理水貯槽、４０・・・洗浄排水貯槽。FIG. 1 is a vertical cross-sectional view showing one embodiment of the present invention, and FIG. 2 is a vertical cross-sectional view showing a conventional example. ■...Flow rate averaging tank, 2...Raw water inflow pipe, 3...
Outflow pipe, 4.16.36...Blower 15, 13, 3
3... Air diffuser pipe, 6... Microorganism adhesion carrier, 10...
Supporting material, 10'... Porous water passing member, 11... Treatment tank, 12.32... Submerged filter bed, 14... Sedimentation separation section,
15... Sludge removal pipe, 17... Overflow launder 18.20
... Valve, 19.37... Treated water outflow pipe, 21...
Washing drainage outflow pipe, 22, 39. 41... pump, 23
...Flocculant injection pipe, 24...Sludge supply pipe, 31...
- Tank, 34... Sedimentation basin, 35... Raw water inflow pipe, 38
... Treated water storage tank, 40... Washing wastewater storage tank.
Claims (3)
した流量平均化槽と、槽内上方部に粒状濾材を充填した
浸漬濾床を保持すると共に該浸漬濾床の内部又は下部に
酸素含有ガスの散気装置を配備し、槽内下方部を沈降分
離部とし、前記浸漬濾床より上方に処理水流出部と洗浄
排水流出部を設けた処理槽とからなり、前記流量平均化
槽の流出部を前記処理槽の沈降分離部に連結し、さらに
前記処理槽の洗浄排水流出部を沈降分離部に連結したこ
とを特徴とする有機性汚水の処理装置。(1) A flow rate averaging tank with a raw water inlet and an outlet and an aeration device installed inside the tank, and an immersed filter bed filled with granular filter media in the upper part of the tank, and inside or below the immersed filter bed. It consists of a treatment tank equipped with an oxygen-containing gas diffuser, a sedimentation separation section in the lower part of the tank, and a treated water outflow section and a washing wastewater outflow section above the immersion filter bed. 1. An apparatus for treating organic sewage, characterized in that an outflow section of a chemical tank is connected to a sedimentation separation section of the treatment tank, and a cleaning wastewater outflow section of the treatment tank is connected to a sedimentation separation section.
を介して沈降分離部に連結した請求項１記載の有機性汚
水の処理装置。(2) The organic sewage treatment apparatus according to claim 1, wherein the cleaning wastewater outflow section of the treatment tank is connected to the sedimentation separation section via the flow rate averaging tank.
前記流量平均化槽に供給する流路を設けた請求項１又は
２記載の有機性汚水の処理装置。(3) The organic sewage treatment apparatus according to claim 1 or 2, further comprising a flow path for supplying a part of the sludge settled in the sedimentation separation section of the treatment tank to the flow rate averaging tank.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2097622A JPH0710393B2 (en) | 1990-04-16 | 1990-04-16 | Organic wastewater treatment equipment |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2097622A JPH0710393B2 (en) | 1990-04-16 | 1990-04-16 | Organic wastewater treatment equipment |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPH03296494A true JPH03296494A (en) | 1991-12-27 |
| JPH0710393B2 JPH0710393B2 (en) | 1995-02-08 |
Family
ID=14197300
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP2097622A Expired - Fee Related JPH0710393B2 (en) | 1990-04-16 | 1990-04-16 | Organic wastewater treatment equipment |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0710393B2 (en) |
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06142692A (en) * | 1992-11-02 | 1994-05-24 | Ebara Infilco Co Ltd | Method and device for purifying organic sewage |
| KR20020067090A (en) * | 2001-02-15 | 2002-08-22 | 주식회사 씨에스엔텍 | Sewage/waste water treating system |
| JP2011020059A (en) * | 2009-07-16 | 2011-02-03 | Kanaiwa:Kk | Water treatment apparatus and water treatment method |
-
1990
- 1990-04-16 JP JP2097622A patent/JPH0710393B2/en not_active Expired - Fee Related
Cited By (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH06142692A (en) * | 1992-11-02 | 1994-05-24 | Ebara Infilco Co Ltd | Method and device for purifying organic sewage |
| KR20020067090A (en) * | 2001-02-15 | 2002-08-22 | 주식회사 씨에스엔텍 | Sewage/waste water treating system |
| JP2011020059A (en) * | 2009-07-16 | 2011-02-03 | Kanaiwa:Kk | Water treatment apparatus and water treatment method |
Also Published As
| Publication number | Publication date |
|---|---|
| JPH0710393B2 (en) | 1995-02-08 |
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