JPS6211636B2 - - Google Patents
Info
- Publication number
- JPS6211636B2 JPS6211636B2 JP18802480A JP18802480A JPS6211636B2 JP S6211636 B2 JPS6211636 B2 JP S6211636B2 JP 18802480 A JP18802480 A JP 18802480A JP 18802480 A JP18802480 A JP 18802480A JP S6211636 B2 JPS6211636 B2 JP S6211636B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- wastewater
- air
- aeration
- contact oxidation
- 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.)
- Expired
Links
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 75
- 238000005273 aeration Methods 0.000 claims description 56
- 230000003647 oxidation Effects 0.000 claims description 50
- 238000007254 oxidation reaction Methods 0.000 claims description 50
- 239000002351 wastewater Substances 0.000 claims description 46
- 238000000034 method Methods 0.000 claims description 17
- 238000004065 wastewater treatment Methods 0.000 claims description 14
- 238000001514 detection method Methods 0.000 claims description 4
- 230000001105 regulatory effect Effects 0.000 claims 1
- 239000010802 sludge Substances 0.000 description 12
- 239000000945 filler Substances 0.000 description 8
- 239000007788 liquid Substances 0.000 description 8
- 238000010586 diagram Methods 0.000 description 7
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 6
- 239000001301 oxygen Substances 0.000 description 6
- 229910052760 oxygen Inorganic materials 0.000 description 6
- 244000005700 microbiome Species 0.000 description 5
- 230000003197 catalytic effect Effects 0.000 description 4
- 230000007423 decrease Effects 0.000 description 4
- 238000007664 blowing Methods 0.000 description 2
- 239000000470 constituent Substances 0.000 description 2
- 239000000463 material Substances 0.000 description 2
- 239000007921 spray Substances 0.000 description 2
- 238000003756 stirring Methods 0.000 description 2
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- QJGQUHMNIGDVPM-UHFFFAOYSA-N nitrogen group Chemical group [N] QJGQUHMNIGDVPM-UHFFFAOYSA-N 0.000 description 1
- 239000004745 nonwoven fabric Substances 0.000 description 1
- 239000010865 sewage Substances 0.000 description 1
- 238000005507 spraying Methods 0.000 description 1
- 238000011144 upstream manufacturing Methods 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
Landscapes
- Biological Treatment Of Waste Water (AREA)
- Treatment Of Biological Wastes In General (AREA)
- Activated Sludge Processes (AREA)
Description
【発明の詳細な説明】
この発明は、有機性廃水を生物的に処理する廃
水処理法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a wastewater treatment method for biologically treating organic wastewater.
一般に有機性廃水の生物学的処理法として、浮
遊式活性汚泥法、ポンプ循環式接触酸化法などが
あり、その前段階として、有機性廃水の原水をそ
の腐敗を防止しつつ貯留する原水貯留調整槽があ
る。この原水貯留調整槽（以下、原水槽と略称す
る）と、上記浮遊式活性汚泥法による曝気槽（以
下、曝気槽と略称する）と、ポンプ循環式接触酸
化法による接触酸化槽（以下、接触酸化槽と略称
する）とは、例えば、原水槽―曝気槽―接触酸化
槽の順に連結して、有機性廃水を処理したり、廃
水濃度が低いなどの場合は、中間の曝気槽を省略
し、原水槽―接触酸化槽と連結し、廃水処理を行
なうことがある。そして従来、上記の原水槽と、
曝気槽および接触酸化槽として、第１図、第２図
および第３図に示す構造のものが知られている。
第１図は、原水槽を示すものである。図中、符号
１は、原水槽であり、この原水槽１には、原水２
が入つており、同原水槽１内の下部に散気部３が
設けられている。この散気部３には、送風機４か
ら散気配管５を介して空気が供給されており、散
気口３ａから原水２中へ散気されている。上記送
風機４と散気部３の間には、流量制御装置６が設
けられており、この流量制御装置６と上記送風機
４との間には、バイパス管７が設けられている。
なお、符号８，９は弁である。また符号１０は流
入原水であり、１１は流れ原水である。ここで、
原水２中へ空気を流通する目的は、原水２の腐敗
防止と撹拌混合である。第２図は曝気槽を示すも
のである。符号２０は曝気槽であり、この曝気槽
２０には廃水と汚泥の混合液２１が満たされてお
り、同曝気槽２０内の下側部に散気口２２ａを有
する散気部２２が設けられている。上記散気部２
２には、第１図に示した原水槽１の場合と同様
に、流量制御装置２３、弁２４、送風機２５が散
気配管２６を介して、流量制御装置２３―弁２４
―送風機２５の順で連結しており、弁２４と送風
機２５の間にはバイパス管２７が設けられてい
る。なお、符号２８は弁であり、２９は流入廃
水、３０は曝気槽処理混合液である。ここで、混
合液２１中には活性汚泥が含まれており、前記散
気部２２の孔２２ａから空気が混合液２１中に流
入されることにより酸素が供給され、混合液２１
の撹拌、循環と相俟つて、廃水２９が処理され
る。第３図は、接触酸化槽を示すもので、符号４
０は接触酸化槽である。この接触酸化槽４０の中
央部には、微生物を固着させるためのプラスチツ
ク成形品、不織布網状品などで成形された充填材
４１が設置されている。４２は流入廃水であり、
この流入廃水４２は、上記接触酸化槽４０に供給
され、槽内廃水４３となる。この槽内廃水４３
は、上記充填材４１を通過し、この充填材４１の
下部に設けられている多数の吸入口４４ａを有す
る抜液部４４に向かう。この抜液部４４からポン
プ４５によつて循環配管４６内に吸入された槽内
廃水４３は、吐出部４７に向い、この吐出部４７
の吐出口４７ａから槽内水面に吐出されている。
この循環過程を経て処理された槽内廃水４３は、
処理水４８となり槽外へ出される。 Generally, biological treatment methods for organic wastewater include floating activated sludge method and pump circulation catalytic oxidation method.As a preliminary step, raw water storage adjustment is performed to store the raw water of organic wastewater while preventing its decay. There is a tank. This raw water storage adjustment tank (hereinafter referred to as the raw water tank), the aeration tank using the floating activated sludge method (hereinafter referred to as the aeration tank), and the contact oxidation tank using the pump circulation type catalytic oxidation method (hereinafter referred to as the contact oxidation tank) (abbreviated as oxidation tank) means, for example, when the raw water tank, aeration tank, and contact oxidation tank are connected in this order to treat organic wastewater, or when the wastewater concentration is low, the intermediate aeration tank can be omitted. , raw water tank - may be connected to a contact oxidation tank to perform wastewater treatment. Conventionally, the above raw water tank and
As aeration tanks and contact oxidation tanks, those having structures shown in FIGS. 1, 2, and 3 are known.
FIG. 1 shows the raw water tank. In the figure, reference numeral 1 is a raw water tank, and this raw water tank 1 includes raw water 2.
is contained, and an aeration section 3 is provided at the lower part of the aquarium tank 1. Air is supplied to this aeration section 3 from a blower 4 via an aeration pipe 5, and is diffused into the raw water 2 from an aeration port 3a. A flow rate control device 6 is provided between the blower 4 and the air diffuser 3, and a bypass pipe 7 is provided between the flow rate control device 6 and the blower 4.
Note that numerals 8 and 9 are valves. Further, numeral 10 is inflow raw water, and 11 is flowing raw water. here,
The purpose of circulating air into the raw water 2 is to prevent spoilage of the raw water 2 and stir and mix it. Figure 2 shows the aeration tank. Reference numeral 20 denotes an aeration tank, and the aeration tank 20 is filled with a mixed liquid 21 of wastewater and sludge, and an aeration section 22 having an aeration port 22a is provided at the lower side of the aeration tank 20. ing. The above air diffuser 2
2, as in the case of the raw water tank 1 shown in FIG.
- A blower 25 is connected in this order, and a bypass pipe 27 is provided between the valve 24 and the blower 25. In addition, the code|symbol 28 is a valve, 29 is inflow waste water, and 30 is an aeration tank treatment mixed liquid. Here, the mixed liquid 21 contains activated sludge, and as air flows into the mixed liquid 21 from the holes 22a of the aeration section 22, oxygen is supplied, and the mixed liquid 21
The waste water 29 is treated together with the stirring and circulation. Figure 3 shows a contact oxidation tank, with reference numeral 4.
0 is a contact oxidation tank. In the center of the contact oxidation tank 40, a filler 41 made of a plastic molded product, a nonwoven fabric reticulated product, or the like is installed for fixing microorganisms. 42 is inflow wastewater;
This inflow wastewater 42 is supplied to the contact oxidation tank 40 and becomes in-tank wastewater 43. This tank wastewater 43
The liquid passes through the filling material 41 and heads toward a liquid extraction section 44 having a large number of suction ports 44a provided at the bottom of the filling material 41. The in-tank wastewater 43 sucked into the circulation pipe 46 by the pump 45 from the draining section 44 is directed toward the discharge section 47 .
It is discharged from the discharge port 47a to the water surface in the tank.
The tank wastewater 43 treated through this circulation process is
It becomes treated water 48 and is discharged outside the tank.
ところで、前記原水槽１と曝気槽２０とにおい
て、同一の送風機と流量制御装置などからなる散
気装置を兼用しようとすると、原水貯留水位に応
じて散気量が変化することになる。一方曝気槽２
０の水位は、常に一定なので、上記のように散気
量が変化することは、曝気槽２０にとつて好まし
くない。従つて、原水槽１用と曝気槽２０用とし
て、それぞれ単独に散気装置を設ける必要が生
じ、そのため従来、原水槽１においては、満水時
に必要とされる送風能力を有する送風機を選定、
設置している。ところが、上記従来の原水槽１に
おいては、原水槽１の水位が低下したときは貯留
原水量が減少し、それにともなつて、必要散気量
は減少するが、送風量は変わらないので、余剰の
空気をバイパス管７から放出することになる。こ
のように、従来の原水槽１は、エネルギーを浪費
しているという欠点を有している。 By the way, if the raw water tank 1 and the aeration tank 20 are to use the same aeration device consisting of an air blower, a flow rate control device, etc., the amount of aeration will change depending on the raw water storage level. On the other hand, aeration tank 2
Since the zero water level is always constant, it is not preferable for the aeration tank 20 that the amount of aeration changes as described above. Therefore, it is necessary to provide separate aeration devices for the raw water tank 1 and the aeration tank 20, and for this reason, conventionally, for the raw water tank 1, a blower with the air blowing capacity required when it is full is selected,
It is installed. However, in the above-mentioned conventional raw water tank 1, when the water level of the raw water tank 1 decreases, the amount of stored raw water decreases, and as a result, the required amount of aeration decreases, but the amount of air blown does not change, so there is no surplus. of air will be released from the bypass pipe 7. As described above, the conventional raw water tank 1 has the disadvantage of wasting energy.
また、一般に廃水の活性汚泥法による処理に際
し、必要な酸素量O2〔Kg／日〕は、概略次式に
よつて算定される。 Further, in general, when treating wastewater by the activated sludge method, the required oxygen amount O 2 [Kg/day] is approximately calculated by the following formula.
O2＝aL＋bS
ここで、Ｌ；除去BOD量〔Kg／日〕
Ｓ＝MLSS〔Kg〕（汚泥量）
ａ，ｂ；係数
ここで、１日を通じ活性廃水（下水）を例にと
れば、流入水量、水質は、第４図のように変化す
る。一般には原水槽１を前置することによつて、
ある程度までこの変動を押える方策がとられてい
るが、充分でなく、かつ夏場と冬場では使用水
量、水質とも異なるのが一般的である。また、曝
気槽内の汚泥濃度（MLSS）を実際上は2000〜
4000ppmの範囲で変化する。送風機２５は、流
入水の汚濁濃度の点からも最大値に近い条件下で
運転出来るだけの能力を備えたものを設置するた
め、実際上は送風能力の１／２以下で充分な時間
帯も割合に多い結果となる。そのため通常は、余
剰空気を槽外へ逃がさないと、槽内が過曝気とな
つて微生物の性状が悪くなり、廃水処理能力が低
下してしまう。従つて通常余剰空気は、バイパス
管２７を通して多かれ少なかれ大気中へ放出され
ており、この放出量は、実際に吹き込まれる空気
量の10〜15％におよんでおり、上記曝気槽２０
は、原水槽１同様、エネルギーを浪費していると
いう欠点を有している。 O 2 = aL + bS Here, L: Amount of BOD removed [Kg/day] S = MLSS [Kg] (Amount of sludge) a, b: Coefficient Here, taking active wastewater (sewage) throughout the day as an example, the inflow Water quantity and quality change as shown in Figure 4. Generally, by placing the raw water tank 1 in front,
Measures have been taken to suppress these fluctuations to some extent, but they are not sufficient, and the amount and quality of water used generally differs between summer and winter. In addition, the sludge concentration (MLSS) in the aeration tank is actually 2000~
Varies in the range of 4000ppm. Since the blower 25 is installed with the ability to operate under conditions close to the maximum value in terms of the pollution concentration of inflow water, in reality, there are times when less than half of the blowing capacity is sufficient. The result is a relatively high percentage. Therefore, unless the excess air is released to the outside of the tank, the inside of the tank will become over-aerated, which will worsen the properties of microorganisms and reduce the wastewater treatment capacity. Therefore, normally, surplus air is more or less released into the atmosphere through the bypass pipe 27, and the amount of this release amounts to 10 to 15% of the amount of air actually blown into the aeration tank 20.
Like raw water tank 1, this has the disadvantage of wasting energy.
また、ポンプ循環式接触酸化法による接触酸化
槽４０が前記した原水槽―曝気槽―接触酸化槽の
ように有機性廃水の処理過程の後の段階において
使用される場合、上記接触酸化槽４０は、以下の
理由により、従来の散気法に比べ優れている。す
なわち、
接触酸化槽４０においては、前に処理過程が
あるので、廃水濃度がそれ程高くなく、処理に
際して多くの酸素を必要としない。 Furthermore, when the contact oxidation tank 40 based on the pump circulation type contact oxidation method is used in a later stage of the organic wastewater treatment process like the above-mentioned raw water tank-aeration tank-contact oxidation tank, the contact oxidation tank 40 is , is superior to conventional aeration methods for the following reasons. That is, in the contact oxidation tank 40, since there is a treatment process beforehand, the concentration of wastewater is not so high and a large amount of oxygen is not required for treatment.
また、後の段階の処理では、一般に汚泥の増
殖が少ないので、接触酸化槽４０の充填材４１
表面で発生増殖する汚泥が少なく、充填材４１
への汚泥付着性が乏しい。従つて廃水の流れが
速いと剥離し処理水質を悪化させる。そのた
め、槽内においては、廃水の流れがゆるやかな
方がよい。 In addition, in the later stages of treatment, the growth of sludge is generally small, so the filler 41 of the contact oxidation tank 40
There is less sludge generated and multiplied on the surface, and the filler 41
Poor sludge adhesion to. Therefore, if the wastewater flows quickly, it will peel off and deteriorate the quality of the treated water. Therefore, it is better for the wastewater to flow slowly in the tank.
一方、散気法による場合、散気量を減少させ
るにつれて、均一に散気することが難しくな
り、従つて均一に廃水を槽内循環させることが
困難になつてくる。 On the other hand, when using the aeration method, as the amount of aeration is reduced, it becomes difficult to diffuse the aeration uniformly, and therefore it becomes difficult to uniformly circulate the wastewater in the tank.
などの理由による。ところが、上記、従来の接触
酸化槽４０は、
○イ 施設費が散気法のみの場合より高くつく。Due to reasons such as. However, the above-mentioned conventional contact oxidation tank 40 has the following problems: (b) The facility cost is higher than when only the aeration method is used.
○ロ 均一に廃水を循環しようと思うと、第５図に
示すように、吐出部４９の配管が非常にめんど
うになり、ポンプなどに圧損がかかる。○B If we try to uniformly circulate the wastewater, as shown in Figure 5, the piping of the discharge section 49 becomes extremely troublesome, and pressure loss is caused to the pump and the like.
○ハ 単位廃水量当りの酸素供給コストが散気法よ
り割高となる。○C The cost of oxygen supply per unit amount of wastewater is higher than that of the aeration method.
などの欠点を有している。また、第５図に示すよ
うに、吐出部４９の配管数および口数を極端に増
すことは、経済的問題から出来ない。従つて、吐
出流速が大きくなり、接触酸化槽内の水面下深く
まで吐出流が入り込んでしまう。このことと、吐
出流の影響を強く受ける範囲内に充填材４１の上
部表面に微生物が付着しなかつたり、付着しても
すぐ剥離したりすることの２つの理由により、ど
うしても充填材４１を水面下40ないし50cm以深に
設置しなければならず、その結果、充填材４１の
槽内充填率が低くなり、接触酸化槽４０のBOD
除去の容積効率が低下してしまうという欠点も生
じてくる。It has drawbacks such as: Further, as shown in FIG. 5, it is not possible to dramatically increase the number of pipes and ports of the discharge section 49 due to economical reasons. Therefore, the discharge flow rate increases, and the discharge flow penetrates deep below the water surface in the contact oxidation tank. For two reasons, this and the fact that microorganisms do not adhere to the upper surface of the filler 41 within the area that is strongly affected by the discharge flow, or that microorganisms peel off immediately even if they do, it is inevitable to remove the filler 41 from the water surface. It must be installed at a depth of 40 to 50 cm or more, and as a result, the filling rate of the filler 41 in the tank becomes low, and the BOD of the catalytic oxidation tank 40 decreases.
Another drawback is that the volumetric efficiency of removal is reduced.
この発明は、上記の事情に鑑みてなされたもの
で、その目的は、原水槽または曝気槽から放出さ
れる余剰エネルギーを有効利用することができ、
接触酸化槽において、施設費および廃水処理コス
トを増やすことなしに廃水処理能力を高めること
ができ、総合的に経済性を向上させることのでき
る有機性廃水の処理法を提供することにあり、原
水槽または曝気槽からでてくる余剰空気を接触酸
化槽に導き、この接触酸化槽に設けるエアリフト
式廃水循環装置に使用することによつて、余剰エ
ネルギーの有効利用をはかり、また接触酸化槽に
通常設けられる吐出部のかわりに接触酸化槽上方
に散水槽を設けて、槽内への循環廃水の流入を均
一にかつ、ゆるやかにすることによつて、経済的
負担なしに、接触酸化槽の処理能力を高めたもの
である。 This invention was made in view of the above circumstances, and its purpose is to make it possible to effectively utilize surplus energy released from a raw water tank or an aeration tank.
Our objective is to provide a method for treating organic wastewater that can increase the wastewater treatment capacity in a contact oxidation tank without increasing facility costs and wastewater treatment costs, and that can improve overall economic efficiency. Excess air coming out of the water tank or aeration tank is guided to the contact oxidation tank and used in the air lift type wastewater circulation device installed in this contact oxidation tank, thereby making effective use of surplus energy. By installing a water sprinkling tank above the contact oxidation tank instead of the discharging section, and making the flow of circulating wastewater into the tank uniform and gradual, the contact oxidation tank can be treated without any economic burden. It is an enhanced ability.
以下、この発明を図面を参照して説明する。 Hereinafter, the present invention will be explained with reference to the drawings.
第６図および第７図は、この発明の実施例を示
すもので、これらの図において、第１図ないし第
３図と同一符号は同一構成要素を示し、その説明
は省略する。 6 and 7 show an embodiment of the present invention. In these figures, the same reference numerals as in FIGS. 1 to 3 indicate the same constituent elements, and the explanation thereof will be omitted.
第６図は、原水槽１―曝気槽２０―接触酸化槽
４０の組み合わせの場合を示すもので、原水槽１
は省略してある。原水槽１からの流れ原水１１
は、流入廃水２９となつて曝気槽内に入つてく
る。バイパス管２７には配管５０が連結されてお
り、接触酸化槽４０へ向つている。この接触酸化
槽４０の上方には散水槽５１が設けられており、
この散水槽５１の底部には多数の小孔が穿設され
ている。散水槽５１は、循環配管４６から槽内廃
水４３が供給されるとともに新らたに設けられた
エアリフト式廃水循環装置５２からも槽内廃水４
３が供給されている。上記エアリフト式廃水循環
装置５２は、槽内下方に設けられた吸入口５３ａ
を有する抜液部５３と、エアリフト配管５４と、
このエアリフト配管５４中に設けられている小散
気部５５とからなる。この小散気部５５は、上記
配管５０に連結されている。また、符号５６は、
散水槽５１内に挿入、設置されているレベルスイ
ツチであり、このレベルスイツチ５６は、ポンプ
４５と連動され、散水槽５１の水位が一定レベル
まで上昇すると、ポンプ４５を停止させ、一定レ
ベルまで低下したら再び作動するように、シーケ
ンスが組まれている。このように構成することに
よつて、曝気槽２０の余剰放出空気は、接触酸化
槽４０のエアリフト式廃水循環装置５２に利用さ
れ、小散気部５５からの散気はエアリフト管５４
内で槽内廃水４３を同伴して上昇し、接触酸化槽
４０の上方に設置した散水槽５１の高さ程度には
揚水力として作用し、しかも散水槽水位の確保に
は循環ポンプ４５の作動に優先して寄与するの
で、無駄がなくなると同時に、エアリフト式循環
による分だけポンプ４５への負荷を減少させるこ
とができるので、経済的である。また、接触酸化
槽４０の上部に多数の穴をあけた散水槽５１を設
けるので、循環のために複雑な配管をしなくても
均一散水均一循環が可能であり、複雑な配管中を
流れることによる圧力損失がなくなるので、エネ
ルギーを節約することができる。そして、経済的
な負担なしに散水口の数を多くとることができる
ので、散水槽５１から槽内への廃水流入はたいへ
んゆるやかになり、充填材４１に付着している微
生物を損うことがない。そのため、充填材を水面
下の浅いところから充填でき、従つて、充填率を
高くとれ、BOD除去の容積効率をあげることが
できる。なお、槽内への廃水流がゆるやかになつ
ても、第８図に示すように、吐出部４７（第３
図）と同一の高さから散水する場合の総括酸素移
動容量係数KLaを比較して見ると、ほとんど同一
の値が得られるので問題はない。 Figure 6 shows the combination of raw water tank 1 - aeration tank 20 - contact oxidation tank 40.
has been omitted. Flow raw water 11 from raw water tank 1
enters the aeration tank as inflow wastewater 29. A piping 50 is connected to the bypass pipe 27 and leads to the catalytic oxidation tank 40 . A water sprinkling tank 51 is provided above this contact oxidation tank 40,
A large number of small holes are bored in the bottom of this water tank 51. The watering tank 51 is supplied with tank wastewater 43 from a circulation pipe 46 and is also supplied with tank wastewater 4 from a newly installed air lift type wastewater circulation device 52.
3 is supplied. The air lift type wastewater circulation device 52 has an inlet 53a provided at the lower part of the tank.
a liquid draining section 53 having an air lift piping 54;
It consists of a small air diffuser 55 provided in this air lift piping 54. This small air diffuser 55 is connected to the piping 50 described above. Moreover, the code 56 is
This is a level switch inserted and installed in the watering tank 51. This level switch 56 is linked with the pump 45, and when the water level in the watering tank 51 rises to a certain level, it stops the pump 45 and lowers it to a certain level. A sequence has been set up so that it will work again after that. With this configuration, excess released air from the aeration tank 20 is utilized for the air lift type waste water circulation device 52 of the contact oxidation tank 40, and aeration from the small aeration section 55 is carried out through the air lift pipe 54.
The water rises along with the waste water 43 inside the tank, and acts as a lifting force to the height of the water spray tank 51 installed above the contact oxidation tank 40, and the circulation pump 45 is operated to maintain the water level in the water spray tank. This is economical because the load on the pump 45 can be reduced by the amount due to the air lift circulation. Furthermore, since the water sprinkling tank 51 with a large number of holes is provided at the top of the contact oxidation tank 40, uniform water spraying and uniform circulation is possible without the need for complicated piping for circulation, and water does not flow through complicated piping. Since there is no pressure loss, energy can be saved. Furthermore, since a large number of water sprinkling ports can be provided without any economical burden, wastewater flows very slowly from the water sprinkling tank 51 into the tank, and microorganisms attached to the filler 41 are not damaged. do not have. Therefore, the filler can be filled from a shallow place below the water surface, and therefore a high filling rate can be achieved, and the volumetric efficiency of BOD removal can be increased. Note that even if the flow of wastewater into the tank becomes slow, the discharge part 47 (third
If you compare the overall oxygen transfer capacity coefficient KLa when watering from the same height as in Figure), you will find almost the same value, so there is no problem.
第７図は、原水槽１―接触酸化槽４０の組み合
わせの場合を示すもので、第６図と同一符号は、
同一構成要素を示し、その説明は省略する。図
中、符号６０は、散気部３と送風機４との間に設
けられた連続流量調節装置であり、この連続流量
調節装置６０は、例えば、弁の開閉が連続的に行
なわれる。電動弁で構成されている。また、符号
６１はレベルスイツチであり、このレベルスイツ
チ６１は、槽中に挿入、設置されており、水位の
昇降にともない連続的に信号を出力する構造を有
しており、この信号は、上記連続流量調節装置６
０へ供給される。信号を供給された上記連続流量
調節装置６０は、供給信号に応じて、流量を調節
し、散気部３で必要とする以外の余剰空気を配管
５０へ流す。この余剰空気は、配管５０を通り、
前記小散気部５５からエアリフト配管５４中へ放
出され、エアリフト循環に利用される。このよう
な構成によつても、前記曝気槽２０―接触酸化槽
４０の場合と同様の作用、利点を発揮することが
できる。 FIG. 7 shows a combination of raw water tank 1 and contact oxidation tank 40, and the same reference numerals as in FIG.
The same constituent elements are shown and their explanation will be omitted. In the figure, reference numeral 60 is a continuous flow rate adjustment device provided between the air diffuser 3 and the blower 4, and in this continuous flow rate adjustment device 60, for example, a valve is continuously opened and closed. Consists of an electric valve. Further, reference numeral 61 is a level switch, which is inserted and installed in the tank and has a structure that continuously outputs a signal as the water level rises and falls. Continuous flow rate adjustment device 6
0. The continuous flow rate adjustment device 60 that has been supplied with the signal adjusts the flow rate in accordance with the supply signal, and allows surplus air other than that required by the air diffuser 3 to flow into the pipe 50. This surplus air passes through the pipe 50,
It is discharged from the small air diffuser 55 into the air lift piping 54 and used for air lift circulation. Even with such a configuration, the same effects and advantages as in the case of the aeration tank 20-catalytic oxidation tank 40 can be exhibited.
なお、曝気槽２０への吹き込み空気量のコント
ロールをこのコントロールをPHなどにより自動的
に行なうようにした先に出願した特願昭54−
140699「含窒素有機性廃水の生物処理装置」に従
つて行なえば、上記曝気槽２０への吹き込み空気
量が最小限にPHなどにより自動的にコントロール
され、曝気槽２０の余剰空気を最大限に取り出す
ことができ、さらに省エネルギー化が図れる。ま
た、上記実施例では、接触酸化槽４０において、
ポンプ４５を一つ設けたが、レベルスイツチ５６
の検出点を増やし、この検出点に対応して作動す
るポンプを、さらに設けてもよい。このようにす
れば、より一層正確に廃水の循環量をコントロー
ルすることができる。さらに、上記のエアリフト
式廃水循環装置５２は、エアリフト配管５４を循
環配管４６に兼用させ、連続配管５０を循環ポン
プ４５の上流または下流に連結する構造に変更す
ることが可能であり、この場合は循環ポンプ４５
の作動には先行しないが、直接駆動エネルギーを
低減させる。 In addition, there is a patent application filed earlier in 1972 in which the amount of air blown into the aeration tank 20 is automatically controlled by pH, etc.
140699 "Biological treatment equipment for nitrogen-containing organic wastewater", the amount of air blown into the aeration tank 20 will be automatically controlled by pH etc. to the minimum, and the surplus air in the aeration tank 20 will be maximized. It can be taken out, further saving energy. Further, in the above embodiment, in the contact oxidation tank 40,
One pump 45 is provided, but the level switch 56
It is also possible to increase the number of detection points and provide a pump that operates corresponding to the detection points. In this way, the amount of waste water circulated can be controlled even more accurately. Furthermore, the air lift type wastewater circulation device 52 described above can be changed to a structure in which the air lift piping 54 is also used as the circulation piping 46 and the continuous piping 50 is connected upstream or downstream of the circulation pump 45. In this case, Circulation pump 45
does not precede the operation of the motor, but directly reduces drive energy.
以上説明したように、この発明に係る廃水処理
法は、原水槽または曝気槽からでてくる余剰空気
を接触酸化槽に導き、この接触酸化槽に設けるエ
アリフト式廃水循環装置に使用することによつ
て、余剰エネルギーの有効利用をはかるととも
に、接触酸化槽に通常設けられる吐出部のかわり
に接触酸化槽の上方に散水槽を設けて、槽内への
循環廃水の流入をゆるやかにすることによつて、
経済的負担なしに、接触酸化槽の処理能力を高め
る方法なので、原水槽または曝気槽から放出され
る余剰エネルギーを有効利用することができ、接
触酸化槽において、施設費および廃水処理コスト
を増やすことなしに廃水処理能力を高めることが
でき、総合的に経済性を向上させるという優れた
利点を有するものである。 As explained above, the wastewater treatment method according to the present invention leads excess air coming out of the raw water tank or the aeration tank to the contact oxidation tank and uses it in the air lift type wastewater circulation device installed in the contact oxidation tank. In addition to making effective use of surplus energy, a water sprinkling tank is installed above the contact oxidation tank instead of the discharge section normally installed in the contact oxidation tank, thereby slowing the flow of circulating wastewater into the tank. Then,
Since this is a method of increasing the processing capacity of a contact oxidation tank without any economic burden, the surplus energy released from the raw water tank or aeration tank can be effectively used, and the facility cost and wastewater treatment cost in the contact oxidation tank can be increased. It has the excellent advantage of increasing wastewater treatment capacity without any wastewater treatment and improving overall economic efficiency.
第１図ないし第３図は、従来の有機性廃水処理
装置を示すもので、第１図は原水槽の説明図、第
２図は曝気槽の説明図、第３図は接触酸化槽の説
明図、第４図はBOD、水量、汚泥物量の経時変
化を示す図、第５図は、吐出部において吐出配管
を多く設けた場合の説明図、第６図および第７図
は、この発明の実施例を示すもので、第６図は、
曝気槽―接触酸化槽の組み合わせの場合の説明
図、第７図は、原水槽―接触酸化槽の組み合わせ
の場合の説明図、第８図は、吐出部と散水槽にお
ける総括酸素移動容量係数を示す図である。
１……原水槽、７，２７……バイパス管、２０
……曝気槽、４０……接触酸化槽、４５……ポン
プ、５０……配管、５１…散水槽、５２……エア
リフト式廃水循環装置、５６……レベルスイツ
チ、６０……連続流量調節装置、６１……レベル
スイツチ。
Figures 1 to 3 show conventional organic wastewater treatment equipment. Figure 1 is an explanatory diagram of the raw water tank, Figure 2 is an explanatory diagram of the aeration tank, and Figure 3 is an illustration of the contact oxidation tank. Figure 4 is a diagram showing changes over time in BOD, water volume, and sludge volume, Figure 5 is an explanatory diagram when a large number of discharge pipes are provided in the discharge section, and Figures 6 and 7 are diagrams showing the changes in BOD, water volume, and sludge volume over time. Fig. 6 shows an example.
An explanatory diagram for the combination of aeration tank and contact oxidation tank. Figure 7 is an explanatory diagram for the combination of raw water tank and contact oxidation tank. Figure 8 shows the overall oxygen transfer capacity coefficient in the discharge section and the watering tank. FIG. 1... Raw water tank, 7, 27... Bypass pipe, 20
... Aeration tank, 40 ... Contact oxidation tank, 45 ... Pump, 50 ... Piping, 51 ... Watering tank, 52 ... Air lift type waste water circulation device, 56 ... Level switch, 60 ... Continuous flow rate adjustment device, 61...Level switch.
Claims (1)
置である原水槽、曝気槽および接触酸化槽を互い
に組み合わせ、連続して廃水を処理する廃水処理
法において、接触酸化槽上方に散水槽を設け、こ
の散水槽に槽内の水位の昇降を検出するレベルス
イツチを設け、このレベルスイツチの検出出力に
応じて、上記接触酸化槽の廃水循環用のポンプが
起動・停止するようにするとともに、散気配管を
介して曝気槽に供給される所定量の空気のうち予
め余剰空気として上記散気配管から放出される空
気を上記接触酸化槽に設けるエアリフト式廃水循
環装置で使われる空気として利用することを特徴
とする廃水処理法。 ２ 原水槽にこの原水槽の槽内の水位の昇降を検
出するレベルスイツチを設け、このレベルスイツ
チの検出出力に応じて、上記原水槽への散気配管
の途中に設ける連続流量調節装置が連動するよう
にするとともに、この連続流量調節装置から放出
される余剰空気を前記接触酸化槽に設けるエアリ
フト式廃水循環装置で使われる空気として利用す
ることを特徴とする特許請求の範囲第１項記載の
廃水処理法。[Scope of Claims] 1 In a wastewater treatment method in which a raw water tank, an aeration tank, and a contact oxidation tank, which are devices for treating organic wastewater by a biological treatment method, are combined with each other to continuously treat wastewater, a contact oxidation tank A water sprinkling tank is provided above, and a level switch is installed in this water sprinkling tank to detect the rise and fall of the water level in the tank, and the pump for circulating waste water in the contact oxidation tank starts and stops according to the detection output of this level switch. In addition, out of the predetermined amount of air supplied to the aeration tank via the aeration pipe, the air released from the aeration pipe as surplus air is used in the air lift type wastewater circulation system installed in the contact oxidation tank. A wastewater treatment method characterized by using the air as wastewater. 2 The raw water tank is equipped with a level switch that detects the rise and fall of the water level in the raw water tank, and a continuous flow rate adjustment device installed in the middle of the aeration pipe to the raw water tank is linked according to the detection output of this level switch. According to claim 1, the surplus air released from the continuous flow rate regulating device is used as air for use in an air lift type waste water circulation device provided in the contact oxidation tank. Wastewater treatment law.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18802480A JPS57107292A (en) | 1980-12-26 | 1980-12-26 | Treatment of waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP18802480A JPS57107292A (en) | 1980-12-26 | 1980-12-26 | Treatment of waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS57107292A JPS57107292A (en) | 1982-07-03 |
| JPS6211636B2 true JPS6211636B2 (en) | 1987-03-13 |
Family
ID=16216320
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP18802480A Granted JPS57107292A (en) | 1980-12-26 | 1980-12-26 | Treatment of waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS57107292A (en) |
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04156375A (en) * | 1990-10-20 | 1992-05-28 | Fuji Photo Film Co Ltd | Thermal printer |
Families Citing this family (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH01249191A (en) * | 1988-03-31 | 1989-10-04 | Tokyu Constr Co Ltd | Method and device for controlling air diffusion rate of variable volume bioreactor |
-
1980
- 1980-12-26 JP JP18802480A patent/JPS57107292A/en active Granted
Cited By (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPH04156375A (en) * | 1990-10-20 | 1992-05-28 | Fuji Photo Film Co Ltd | Thermal printer |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS57107292A (en) | 1982-07-03 |
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