JPH0947781A - Treatment of organic material related to bod, nitrogen and phosphorus in waste water - Google Patents
Treatment of organic material related to bod, nitrogen and phosphorus in waste waterInfo
- Publication number
- JPH0947781A JPH0947781A JP7205507A JP20550795A JPH0947781A JP H0947781 A JPH0947781 A JP H0947781A JP 7205507 A JP7205507 A JP 7205507A JP 20550795 A JP20550795 A JP 20550795A JP H0947781 A JPH0947781 A JP H0947781A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- tank
- aeration tank
- anaerobic
- fiber membrane
- 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.)
- Pending
Links
Landscapes
- Separation Using Semi-Permeable Membranes (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
- Treatment Of Sludge (AREA)
Abstract
Description
【０００１】[0001]
【発明の属する技術分野】本発明は、生活系、産業系を
問わず、有機物を含む廃水の処理に利用されて、ＢＯ
Ｄ、窒素および燐の高度処理が可能で、かつ、効率の良
い生物学的廃水処理方法に関する。BACKGROUND OF THE INVENTION 1. Field of the Invention The present invention is used for treating wastewater containing organic matter, regardless of whether it is a living system or an industrial system.
The present invention relates to a biological wastewater treatment method capable of performing advanced treatment of D, nitrogen and phosphorus and being efficient.
【０００２】[0002]
【従来の技術】従来法における典型的な生物学的廃水処
理技術は、図２に示されるようなものであり、それによ
ると、原水（処理廃水）は、一旦調整槽に送られた後に
曝気槽に移され、こゝで所定の生物学的処理に付され
る。次いで、処理液は沈殿槽へ移され、そこで汚泥と処
理水に沈降分離され、処理水は更に必要な無害化処理等
が施されて河川等へ放出され、一方、汚泥はその一部が
返送汚泥として曝気槽へと戻されると共に、その大部分
は脱水機により汚泥ケーキと脱離液とに分離される。2. Description of the Related Art A typical biological wastewater treatment technique in the conventional method is as shown in FIG. 2, according to which raw water (treated wastewater) is aerated once sent to a regulating tank. It is transferred to a tank and subjected to a predetermined biological treatment there. Next, the treated liquid is transferred to a settling tank, where it is separated into sludge and treated water, and the treated water is further subjected to necessary detoxification treatment, etc., and discharged to rivers, etc. The sludge is returned to the aeration tank, and most of it is separated into a sludge cake and a desorbed liquid by a dehydrator.
【０００３】このように、従来法では、一般に処理に関
与する微生物（汚泥）と処理水を分離するのに沈殿法を
採用しているので、処理槽（曝気槽）内の汚泥濃度をあ
まり高くできず、通常２０００〜５０００mg／ｌ程度に
維持している。As described above, in the conventional method, since the precipitation method is generally used to separate the microorganisms (sludge) involved in the treatment from the treated water, the sludge concentration in the treatment tank (aeration tank) is too high. It is not possible, and usually it is maintained at about 2000 to 5000 mg / l.
【０００４】また、沈殿槽内でも、僅かな条件変動によ
って微生物の状態が変わり、沈降不良となるので、日常
管理には多大な注意を払っているにもかかわらず、しば
しば汚泥のリークによる水質悪化をきたしている。Even in the settling tank, slight changes in conditions change the state of microorganisms, resulting in poor sedimentation. Therefore, despite great care in daily management, water quality often deteriorates due to sludge leaks. Is coming.
【０００５】また、廃水の生物学的処理において、嫌気
部と好気部を組み合わせることによって、脱窒、脱燐の
効率を上げる方法も周知の技術である。Further, in biological treatment of wastewater, a method of increasing the efficiency of denitrification and dephosphorization by combining an anaerobic part and an aerobic part is a well-known technique.
【０００６】好気部で十分硝化されたものを嫌気部に導
いてそれにＢＯＤ成分を含む原水を投入すると、脱窒が
起こり、窒素ガスとして大気中に放出される。また、余
剰汚泥の系外排出によって脱燐が達成されるが、そのメ
カニズムは、活性汚泥を好気と嫌気の交互処理に付する
と、ある種の微生物は、嫌気部において通常よりも多く
の燐を細胞外に排出し、また、好気部においては逆に過
剰の燐分を体内に取り込むことにある。したがって、嫌
気部と好気部を移動させながら好気部において汚泥を引
き抜けば、効率の良い脱燐が達成されることになる。When what is sufficiently nitrified in the aerobic part is introduced into the anaerobic part and the raw water containing the BOD component is added thereto, denitrification occurs and is released into the atmosphere as nitrogen gas. Dephosphorization is achieved by discharging excess sludge out of the system. The mechanism is that when activated sludge is subjected to alternate treatment of aerobic and anaerobic, certain microorganisms cause more phosphorus than usual in the anaerobic part. Is excreted outside the cells, and in the aerobic region, on the contrary, excessive phosphorus is taken into the body. Therefore, if sludge is pulled out in the aerobic part while moving the anaerobic part and the aerobic part, efficient dephosphorization can be achieved.
【０００７】しかしながら、従来法では、せっかく好気
の曝気槽から汚泥を引き抜いても、脱水して固形物とす
る前に、沈殿槽、汚泥濃縮槽等の静置を要する工程を経
る関係上、その間に汚泥が嫌気性となり、取り込んだ燐
を一部体外に排出する結果、脱燐効率を低下させている
場合が多い。However, in the conventional method, even if the sludge is drawn out from the aerobic aeration tank, it is necessary to leave the settling tank, the sludge thickening tank and the like still before dewatering to make solid matter. During that time, the sludge becomes anaerobic, and some of the incorporated phosphorus is discharged out of the body, resulting in a decrease in the dephosphorization efficiency in many cases.
【０００８】[0008]
【発明が解決しようとする課題】本発明の目的は、曝気
槽内での汚泥濃度を高く維持して、効率的な廃水処理を
可能となすような廃水処理方法を提供することにある。SUMMARY OF THE INVENTION An object of the present invention is to provide a wastewater treatment method which enables efficient treatment of wastewater by maintaining a high sludge concentration in the aeration tank.
【０００９】また、本発明の目的は、汚泥の沈降性に左
右されず、常に安定した処理水を得る廃水処理方法を提
供することにある。Another object of the present invention is to provide a wastewater treatment method which always obtains treated water that is stable regardless of sludge sedimentation.
【００１０】さらに、本発明の目的は、好気状態の汚泥
を速やかに脱水して、脱燐効果を上げる廃水処理方法を
提供することにある。A further object of the present invention is to provide a wastewater treatment method for rapidly dehydrating aerobic sludge to enhance the dephosphorization effect.
【００１１】[0011]
【課題を解決するための手段】即ち、本発明は、処理廃
水を嫌気槽に導入し、汚泥を曝気槽と嫌気槽との間で循
環移動させつつ行う生物学的廃水処理方法において、前
記嫌気槽では脱窒を行うと共に、前記曝気槽では、その
汚泥濃度（ＭＬＳＳ）を５０００mg／Ｌ以上に維持し
て、この曝気槽内に浸漬設置した中空糸膜モジュールに
よって処理水を直接吸引、濾過分離する一方、当該曝気
槽から汚泥を引抜いて、直ちに脱水機によって固液分離
して汚泥の脱水ケーキとなすことを特徴とする廃水中の
ＢＯＤ、窒素および燐の処理方法にある。That is, the present invention relates to a biological wastewater treatment method in which treated wastewater is introduced into an anaerobic tank and sludge is circulated between the aeration tank and the anaerobic tank. Denitrification is performed in the tank, and the sludge concentration (MLSS) in the aeration tank is maintained at 5000 mg / L or more, and the treated water is directly sucked and filtered by the hollow fiber membrane module immersed in the aeration tank. On the other hand, in the method for treating BOD, nitrogen and phosphorus in wastewater, the sludge is drawn out from the aeration tank and immediately solid-liquid separated by a dehydrator to form a dehydrated cake of sludge.
【００１２】特に、本発明の前記廃水の処理方法におい
ては、処理に関与する微生物（汚泥）と処理水とを分離
する手段として、曝気槽内に直接浸漬した中空糸膜モジ
ュールを採用した点に特徴を有し、その中空糸膜に分画
能が０．００５〜０．５μｍのものを用いると、膜を透
過した処理水は常に清澄な状態のものが得られる。In particular, in the method for treating wastewater of the present invention, the hollow fiber membrane module directly immersed in the aeration tank is adopted as a means for separating the microorganisms (sludge) involved in the treatment from the treated water. When a hollow fiber membrane having a characteristic and a fractionation capacity of 0.005 to 0.5 μm is used, the treated water that has permeated the membrane is always in a clear state.
【００１３】また、本発明では、曝気槽より引き抜いた
汚泥は、沈殿槽を経ることなく、直接脱水機にかけるこ
とにも特徴を有する。こゝでの順調な脱水が維持される
ため、脱水機での汚泥濃度は５０００mg／Ｌ以上（好ま
しくは、８０００〜３０，０００mg／Ｌ、最も好ましく
は、１０，０００〜１５，０００mg／Ｌ）に維持する。The present invention is also characterized in that the sludge extracted from the aeration tank is directly applied to the dehydrator without passing through the sedimentation tank. Sludge concentration in the dehydrator is 5000 mg / L or more (preferably 8000 to 30,000 mg / L, most preferably 10,000 to 15,000 mg / L) because smooth dehydration is maintained here. To maintain.
【００１４】[0014]
【発明の実施の形態】以下、本発明を図１に示したフロ
ーシートに基づき具体的に説明する。BEST MODE FOR CARRYING OUT THE INVENTION The present invention will be described in detail below with reference to the flow sheet shown in FIG.
【００１５】処理廃水（原水）は、原水槽（１）に一時
貯留された後、原水ポンプ（２）によりスクリーン
（３）を介して嫌気槽（４）中に送液される。嫌気槽
（４）内では、撹拌ポンプ（５）によって原水と汚泥と
がゆっくり撹拌、旋回されつつ嫌気処理が行われる。そ
こでの被処理水の一部は、汚泥と共に連通管（６）を通
って曝気槽（９）へと運ばれ、また、曝気槽（９）内で
好気処理された汚泥水の一部は、返送ポンプ（７）によ
り返送管（８）を介して嫌気槽（４）に返送され、これ
ら嫌気槽と曝気槽間に循環流が形成される。そうする
と、曝気槽（９）の好気部で十分硝化（有機−Ｎ→ＮＯ
3 - ，ＮＨ4 + →ＮＯ3 - ）された汚泥が嫌気槽（４）
内で原水と混合して脱窒（ＮＯ3 - →Ｎ2 ↑）が起こ
り、嫌気槽（４）からＮ2 ガスが大気中に放散される。The treated wastewater (raw water) is temporarily stored in the raw water tank (1) and then sent to the anaerobic tank (4) by the raw water pump (2) through the screen (3). In the anaerobic tank (4), raw water and sludge are slowly stirred and swirled by the stirring pump (5) to perform anaerobic treatment. A part of the water to be treated there is carried to the aeration tank (9) through the communication pipe (6) together with the sludge, and a part of the sludge water aerobically treated in the aeration tank (9) is Is returned by the return pump (7) to the anaerobic tank (4) via the return pipe (8), and a circulating flow is formed between these anaerobic tank and aeration tank. Then, in the aerobic part of the aeration tank (9), sufficient nitrification (organic-N → NO
3 -, NH 4 + → NO 3 -) sludge is anaerobic tank (4)
Denitrification is mixed with raw water in the inner (NO 3 - → N 2 ↑ ) occurs, N 2 gas is dissipated into the atmosphere from the anaerobic tank (4).
【００１６】次に、曝気槽（９）内には、中空糸膜モジ
ュール（１０）および散気管（１２）が設置され、こゝ
での汚泥水が曝気処理に付されると共に、該中空糸膜モ
ジュール（１０）により、処理水が吸引ポンプ（１４）
を介して吸引、濾過分離される。曝気槽（９）の水面
は、フロート１３によって一定に維持されている。この
曝気槽（９）内の汚泥濃度は、通常８０００〜３０，０
００mg／Ｌに維持されるが、前記中空糸膜モジュール
（１０）を用いて曝気槽（９）内で直接処理水を分離し
ているので、汚泥の沈降性に左右されずに常に安定して
処理水を得ることができ、また、中空糸膜も、分画能
０．００５〜０．５μｍのものを用いているので、直接
常に清澄な状態のものが得られる。さらに、吸引ポンプ
（１４）は、通常−０．０５〜−０．３kg／cm2 で運転
されるので、中空糸膜モジュール（１０）が吸引力大の
ため破壊されることもない。処理水は、流量計（１５）
によって常に特定の水量が得られるようにされている。Next, in the aeration tank (9), a hollow fiber membrane module (10) and an air diffuser pipe (12) are installed, and the sludge water is subjected to aeration treatment, and the hollow fiber The membrane module (10) allows the treated water to be a suction pump (14).
It is suctioned through and separated by filtration. The water surface of the aeration tank (9) is kept constant by the float 13. The sludge concentration in this aeration tank (9) is usually 8,000 to 30,0.
Although it is maintained at 00 mg / L, since the treated water is directly separated in the aeration tank (9) using the hollow fiber membrane module (10), it is always stable regardless of the sludge settling property. Treated water can be obtained, and since the hollow fiber membrane having a fractionation capacity of 0.005 to 0.5 μm is used, a clear state can be obtained directly. Furthermore, since the suction pump (14) is normally operated at -0.05 to -0.3 kg / cm 2 , the hollow fiber membrane module (10) is not destroyed due to its large suction force. Treated water flow meter (15)
Ensures that a certain amount of water is always obtained.
【００１７】前記の曝気槽（９）での好気部において、
汚泥水中の燐成分は、汚泥中の微生物の作用により有機
燐に変えられ（ＰＯ4 3- →有機−Ｐ）、これを微生物が
過剰に体内に取り込む結果、好気部にある汚泥は多量の
燐分を含む。この汚泥の一部が、曝気槽（９）から汚泥
引抜ポンプ（１１）によって直接引き抜かれ、これに経
路途中のラインミキサー（１８）中で凝集剤（ポリ硫酸
第２鉄）が投入、混和された後に、脱水機（２１）に導
びかれ、そこで直ちに固液分離されて脱水ケーキ（２
４）と脱離液とに分離される。脱離液は、返送ポンプ
（２３）によって曝気槽（９）へと返送されるが、脱水
ケーキ（２４）は、その後廃棄される。そうすると、こ
の脱水ケーキ（２４）には、前述のように多量の燐成分
が含まれ、また、この脱水ケーキ（２４）は、従来法の
如く、活性汚泥としてその一部が返送再使用されること
がないので、本発明では、燐の高度処理を効率的に活用
することが可能となる。In the aerobic section of the aeration tank (9),
Phosphorus component of the sludge water, is changed to an organic phosphorous by the action of microorganisms in the sludge (PO 4 3- → Organic -P), which microorganism is excessively taken into the body result, sludge in the aerobic part of the large amount Contains phosphorus. A part of this sludge is directly drawn from the aeration tank (9) by the sludge drawing pump (11), and the coagulant (ferric polysulfate) is added and mixed in the line mixer (18) on the way to this. After that, it is guided to a dehydrator (21), where it is immediately subjected to solid-liquid separation and dehydrated cake (2
4) and the desorbed liquid are separated. The desorbed liquid is returned to the aeration tank (9) by the return pump (23), but the dehydrated cake (24) is thereafter discarded. Then, the dehydrated cake (24) contains a large amount of phosphorus component as described above, and the dehydrated cake (24) is partially returned and reused as activated sludge as in the conventional method. Therefore, the present invention enables efficient use of advanced phosphorus treatment.
【００１８】前記の脱水機（２１）には、図示のベルト
フィルター式のものあるいは遠心脱水式のもの等、速や
かに固液分離し得るものならば使用可能であり、また、
前記処理水の一部をこの脱水機（２１）の洗浄水に使用
するようにしてもよい。The dehydrator (21) may be of any type, such as the belt filter type or centrifugal dehydration type shown in the figure, as long as it can rapidly perform solid-liquid separation.
A part of the treated water may be used as washing water for the dehydrator (21).
【００１９】[0019]
【実施例】本発明方法を食品加工工場（大豆加工工場）
の廃水処理に適用した事例を、以下実施例として示す。 （１）処理設備：図１のフローシート参照 曝気槽…４０m3 嫌気槽…４０m3 （２）処理水量：３０m3／day （３）原水水質：ＢＯＤ…２０００〜３０００mg／Ｌ ＣＯＤ…１０００〜２０００mg／Ｌ Ｔ−Ｎ…２００〜３００mg／Ｌ Ｔ−Ｐ…２０〜４０mg／Ｌ ＳＳ…１０００〜２０００mg／Ｌ （４）運転状況：ＭＬＳＳ…１０，０００〜１５，０００mg／Ｌ 汚泥引抜量…１０〜２０kg／day （固形物当り） ４０〜８０kg／day （７０％含水ケーキ当り） ケーキ中のＰ含有量…５．５％（乾燥重量当り） （５）処理水水質：ＢＯＤ…５〜１５mg／Ｌ ＣＯＤ…２０〜５０mg／Ｌ Ｔ−Ｎ…５〜１０mg／Ｌ Ｔ−Ｐ…０．２〜１．０mg／Ｌ ＳＳ…０〜５mg／Ｌ[Example] The method of the present invention is applied to a food processing factory (soybean processing factory).
An example applied to the wastewater treatment of is shown below as an example. (1) processing equipment: flowsheet refer aeration tank ... 40 m 3 anaerobic tank ... 40 m 3 (2) of treated water in Figure 1: 30 m 3 / day (3) raw water quality: BOD ... 2000~3000mg / L COD ... 1000~2000mg /LT-N...200-300 mg / LT-P ... 20-40 mg / L SS ... 1000-2000 mg / L (4) Operation status: MLSS ... 10,000-15,000 mg / L Sludge draw-off ... 10 20 kg / day (per solid) 40-80 kg / day (per 70% water-containing cake) P content in the cake: 5.5% (per dry weight) (5) Treated water quality: BOD: 5-15 mg / L COD ... 20-50 mg / L T-N ... 5-10 mg / L T-P ... 0.2-1.0 mg / L SS ... 0-5 mg / L
【００２０】[0020]
【発明の効果】本発明の廃水処理方法を導入することに
より、次の利点が得られる。 （１）中空糸膜モジュールにより曝気槽より直接処理水
を得る方法であるので、汚泥の沈降性に左右されずに常
に安定した処理水を得ることができる。 （２）曝気槽より引き抜いた汚泥を直ちに脱水機により
固液分離する方法であるので、効率の良い脱燐処理が可
能である。 （３）従来法のように、調整槽や沈殿槽等の設備が不要
であるので、付帯設備を大巾に削減でき、所要敷地面積
が小さくて済む。 （４）中空糸膜モジュールおよび脱水槽の運転・管理
は、複雑でないので、本発明方法全体システムの維持管
理が極めて容易である。The following advantages are obtained by introducing the wastewater treatment method of the present invention. (1) Since the treated water is directly obtained from the aeration tank by the hollow fiber membrane module, stable treated water can be always obtained without being affected by the sludge settling property. (2) Since the sludge drawn out from the aeration tank is immediately subjected to solid-liquid separation by a dehydrator, efficient dephosphorization treatment is possible. (3) Unlike the conventional method, no equipment such as an adjusting tank and a sedimentation tank is required, so that auxiliary equipment can be greatly reduced and the required site area can be reduced. (4) Since the operation and management of the hollow fiber membrane module and the dehydration tank are not complicated, maintenance of the entire system of the present invention is extremely easy.
【図１】本発明の廃水処理法のフローシート図である。FIG. 1 is a flow sheet diagram of a wastewater treatment method of the present invention.
【図２】従来の廃水処理法のフローシート図である。FIG. 2 is a flow sheet diagram of a conventional wastewater treatment method.
１…原水槽 ２…原水ポンプ ３…スクリーン ４…嫌気槽 ５…撹拌ポンプ ６…連通管 ７…返送ポンプ ８…返送管 ９…曝気槽 １０…中空糸膜モジュール １１…汚泥引抜ポンプ １２…散気管 １３…フロートスイッチ １４…吸引ポンプ １５…流量計 １６…洗浄水貯槽 １７…洗浄水圧送ポンプ １８…ラインミキサー １９…凝集液貯槽 ２０…凝集液送液ポンプ ２１…脱水機 ２２…脱離液貯槽 ２３…脱離液返送ポンプ ２４…脱水ケーキ 1 ... Raw water tank 2 ... Raw water pump 3 ... Screen 4 ... Anaerobic tank 5 ... Stirring pump 6 ... Communication pipe 7 ... Return pump 8 ... Return pipe 9 ... Aeration tank 10 ... Hollow fiber membrane module 11 ... Sludge extraction pump 12 ... Diffuser pipe 13 ... Float switch 14 ... Suction pump 15 ... Flow meter 16 ... Wash water storage tank 17 ... Wash water pressure pump 18 ... Line mixer 19 ... Aggregate liquid storage tank 20 ... Aggregate liquid supply pump 21 ... Dehydrator 22 ... Desorption liquid storage tank 23 … Desorption liquid return pump 24… Dehydrated cake
Claims (3)
槽と嫌気槽との間で循環移動させつつ行う生物学的廃水
処理方法において、前記嫌気槽では脱窒を行うと共に、
前記曝気槽では、その汚泥濃度（ＭＬＳＳ）を５０００
mg／Ｌ以上に維持して、この曝気槽内に浸漬設置した中
空糸膜モジュールによって処理水を直接吸引、濾過分離
する一方、当該曝気槽から汚泥を引抜いて、直ちに脱水
機によって固液分離して汚泥の脱水ケーキとなすことを
特徴とする廃水中のＢＯＤ、窒素および燐の処理方法。1. A biological wastewater treatment method in which treated wastewater is introduced into an anaerobic tank and sludge is circulated between an aeration tank and an anaerobic tank, and denitrification is performed in the anaerobic tank,
In the aeration tank, the sludge concentration (MLSS) is set to 5000
The treated water is directly sucked and filtered by the hollow fiber membrane module immersed and installed in the aeration tank while maintaining the amount of mg / L or more, while the sludge is pulled out from the aeration tank and immediately solid-liquid separated by the dehydrator. A method for treating BOD, nitrogen and phosphorus in wastewater, which comprises forming a dehydrated cake of sludge.
分画能が０．００５〜０．５μｍである中空糸膜を用い
ることを特徴とする請求項１に記載の方法。2. The method according to claim 1, wherein a hollow fiber membrane having a fractionation capacity of 0.005 to 0.5 μm is used in the hollow fiber membrane module.
を８０００〜３０，０００ｇ／Ｌに維持することを特徴
とする請求項１に記載の方法。3. Sludge concentration (MLSS) in the aeration tank
Is maintained between 8000 and 30,000 g / L.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7205507A JPH0947781A (en) | 1995-08-11 | 1995-08-11 | Treatment of organic material related to bod, nitrogen and phosphorus in waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7205507A JPH0947781A (en) | 1995-08-11 | 1995-08-11 | Treatment of organic material related to bod, nitrogen and phosphorus in waste water |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| JPH0947781A true JPH0947781A (en) | 1997-02-18 |
Family
ID=16508015
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7205507A Pending JPH0947781A (en) | 1995-08-11 | 1995-08-11 | Treatment of organic material related to bod, nitrogen and phosphorus in waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPH0947781A (en) |
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100412330B1 (en) * | 2002-10-25 | 2004-01-07 | 주식회사 진우환경기술연구소 | Membrane Coupled Activated Sludge Method Operating Anoxic/Anaerobic Zone alternatively for Removal of Nitrogen and Phosphorus |
| KR100435107B1 (en) * | 2001-10-29 | 2004-06-09 | 교우산업개발(주) | Advance Treatment Equipment and Process for Nitrogen and Phosphate Removal in Sewage and Wastewater |
| JP2005103381A (en) * | 2003-09-29 | 2005-04-21 | Hitachi Plant Eng & Constr Co Ltd | Method and apparatus for nitrification |
| JP2006052096A (en) * | 2004-08-10 | 2006-02-23 | Kubota Corp | Method of manufacturing liquid fertilizer |
| CN1318320C (en) * | 2004-04-21 | 2007-05-30 | 中国科学院生态环境研究中心 | H circulation pipe separated type membrane bioreactor |
| JP2008259990A (en) * | 2007-04-13 | 2008-10-30 | Sanritsu Kakoki Kk | Waste water treatment system and waste water treatment method |
| US11624514B2 (en) * | 2019-02-03 | 2023-04-11 | Gd Midea Air-Conditioning Equipment Co., Ltd. | Window air conditioner with water receiving pan and filter screen support |
-
1995
- 1995-08-11 JP JP7205507A patent/JPH0947781A/en active Pending
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| KR100435107B1 (en) * | 2001-10-29 | 2004-06-09 | 교우산업개발(주) | Advance Treatment Equipment and Process for Nitrogen and Phosphate Removal in Sewage and Wastewater |
| KR100412330B1 (en) * | 2002-10-25 | 2004-01-07 | 주식회사 진우환경기술연구소 | Membrane Coupled Activated Sludge Method Operating Anoxic/Anaerobic Zone alternatively for Removal of Nitrogen and Phosphorus |
| JP2005103381A (en) * | 2003-09-29 | 2005-04-21 | Hitachi Plant Eng & Constr Co Ltd | Method and apparatus for nitrification |
| CN1318320C (en) * | 2004-04-21 | 2007-05-30 | 中国科学院生态环境研究中心 | H circulation pipe separated type membrane bioreactor |
| JP2006052096A (en) * | 2004-08-10 | 2006-02-23 | Kubota Corp | Method of manufacturing liquid fertilizer |
| JP2008259990A (en) * | 2007-04-13 | 2008-10-30 | Sanritsu Kakoki Kk | Waste water treatment system and waste water treatment method |
| US11624514B2 (en) * | 2019-02-03 | 2023-04-11 | Gd Midea Air-Conditioning Equipment Co., Ltd. | Window air conditioner with water receiving pan and filter screen support |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| US4749494A (en) | Treatment of waste water by the activated sludge process | |
| CN114291964B (en) | Sewage treatment system and method for denitrification and phosphorus recovery | |
| JPS6210720B2 (en) | ||
| KR19980083279A (en) | Treatment method of high concentration organic wastewater and nutrients using immersion type microfiltration membrane-activated sludge process | |
| JPS5845920B2 (en) | Biochemical treatment method for organic waste liquid | |
| JPH0947781A (en) | Treatment of organic material related to bod, nitrogen and phosphorus in waste water | |
| JP3368938B2 (en) | Wastewater treatment method and apparatus | |
| JP2796909B2 (en) | Wastewater treatment method | |
| EP0822165B1 (en) | Method for the treatment of waste water | |
| JPH0722757B2 (en) | Biological removal method of nitrogen and phosphorus and its treatment device | |
| KR102108870B1 (en) | Membrane Treatment Device for Eliminating Nitrogen and/or Phosphorus | |
| CA2425147A1 (en) | Apparatus and method for wastewater treatment with enhanced solids reduction (esr) | |
| JP3843540B2 (en) | Biological treatment method of effluent containing organic solids | |
| JP2000107797A (en) | Purification method and apparatus | |
| KR960011888B1 (en) | Method and apparatus for biological treatment of waste water including nitrogen and phosphorus | |
| JPH0483594A (en) | Biological treatment of organic sewage | |
| JP2001179284A (en) | Method for dephosphorizing excretion wastewater | |
| JP3369915B2 (en) | Night soil treatment equipment | |
| JPS643557B2 (en) | ||
| JP3326084B2 (en) | How to reduce organic sludge | |
| JPH0649199B2 (en) | Human waste system treatment equipment | |
| RU2743531C1 (en) | Method of biological purification of liquid fractions containing a disinfectant quaternary ammonium salts (qac) and similar substances together with household and/or industrial wastewater close to them in composition | |
| JP3229806B2 (en) | Human wastewater treatment equipment | |
| JPH105762A (en) | Activated sludge process and device therefor | |
| JPH05192694A (en) | Sewage treatment method |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| A131 | Notification of reasons for refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A131 Effective date: 20040224 |
|
| A02 | Decision of refusal |
Free format text: JAPANESE INTERMEDIATE CODE: A02 Effective date: 20040713 |