JPS596996A - Treatment of organic filthy water of high concentration - Google Patents
Treatment of organic filthy water of high concentrationInfo
- Publication number
- JPS596996A JPS596996A JP11399782A JP11399782A JPS596996A JP S596996 A JPS596996 A JP S596996A JP 11399782 A JP11399782 A JP 11399782A JP 11399782 A JP11399782 A JP 11399782A JP S596996 A JPS596996 A JP S596996A
- Authority
- JP
- Japan
- Prior art keywords
- sludge
- tank
- liquid
- denitrification
- returned
- 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 abstract description 17
- 239000010802 sludge Substances 0.000 claims abstract description 51
- 239000007788 liquid Substances 0.000 claims abstract description 37
- 238000000034 method Methods 0.000 claims description 32
- 238000000926 separation method Methods 0.000 claims description 16
- 239000002351 wastewater Substances 0.000 claims description 8
- 238000005273 aeration Methods 0.000 claims description 7
- 238000004062 sedimentation Methods 0.000 claims description 5
- 230000005484 gravity Effects 0.000 claims description 3
- 238000005188 flotation Methods 0.000 claims description 2
- 238000005119 centrifugation Methods 0.000 claims 1
- 239000002562 thickening agent Substances 0.000 abstract description 7
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 abstract description 5
- 238000000746 purification Methods 0.000 abstract description 5
- 229910001873 dinitrogen Inorganic materials 0.000 abstract description 3
- 239000007789 gas Substances 0.000 abstract description 2
- 229910002651 NO3 Inorganic materials 0.000 abstract 2
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 abstract 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 abstract 1
- 230000002708 enhancing effect Effects 0.000 abstract 1
- 229910052757 nitrogen Inorganic materials 0.000 abstract 1
- 239000002689 soil Substances 0.000 abstract 1
- 241000894006 Bacteria Species 0.000 description 3
- JVMRPSJZNHXORP-UHFFFAOYSA-N ON=O.ON=O.ON=O.N Chemical compound ON=O.ON=O.ON=O.N JVMRPSJZNHXORP-UHFFFAOYSA-N 0.000 description 3
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical compound [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 3
- 239000010800 human waste Substances 0.000 description 3
- 239000010865 sewage Substances 0.000 description 3
- 239000006228 supernatant Substances 0.000 description 3
- 230000001546 nitrifying effect Effects 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 1
- 238000007796 conventional method Methods 0.000 description 1
- 238000010790 dilution Methods 0.000 description 1
- 239000012895 dilution Substances 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 238000012423 maintenance Methods 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 239000000243 solution Substances 0.000 description 1
- 241000894007 species Species 0.000 description 1
- 210000002700 urine Anatomy 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
【発明の詳細な説明】
本発明は、曝気槽の活性汚泥を高濃度に維持して汚水の
高負荷処理を行う方法に関するものである。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a method for high-load treatment of sewage by maintaining activated sludge in an aeration tank at a high concentration.
従来、し尿系汚水などの有機性汚水を脱窒素を目的とし
て活性汚泥法で処理する場合、処理槽内のＭＬＳＳ濃度
を２０００〜５０００〜Ａに維持してなされていたが、
近年処理効率を高めるために、処理槽内のＭＬＳＳ濃度
を１００００〜２００００ ＴｒｌｆＡと高くする方法
が種々研究されている。Conventionally, when organic sewage such as human waste sewage was treated by the activated sludge method for the purpose of denitrification, the MLSS concentration in the treatment tank was maintained at 2000-5000-A.
In recent years, various methods of increasing the MLSS concentration in the treatment tank to 10,000 to 20,000 TrlfA have been studied in order to improve treatment efficiency.
このような生物処理においては、生物処理後に固液の分
離が行われるが、処理槽内の汚泥濃度を高くすると固液
分離工程において汚泥の沈降性が悪くなシ、沈殿槽の水
面積を大きくする必要がある。また汚泥濃度が高いため
に汚泥の安定性を欠き、時々汚泥が上澄液と共に流出す
ることがある。In this type of biological treatment, solid-liquid separation is performed after biological treatment, but if the sludge concentration in the treatment tank is increased, the settling of the sludge will be poor in the solid-liquid separation process, and the water area of the settling tank must be increased. There is a need to. Furthermore, due to the high sludge concentration, the sludge lacks stability, and the sludge sometimes flows out together with the supernatant liquid.
このような問題に対処するため従来第１図、第２図に示
すような方法が提案されている。すなわち！＠１図の方
法は、汚水１０を曝気槽銀で処理し、沈殿槽（９）で固
液分離したのち遠心分離機４０で清澄化処理し処理水５
０とするものであり、第２図の方法は曝気槽銀からの流
出液を全量遠心分離機４０で処理するものである。なお
、■は返送汚泥である。In order to deal with such problems, methods as shown in FIGS. 1 and 2 have been proposed. That is! In the method shown in Figure @1, wastewater 10 is treated in an aeration tank (9), solid-liquid separation is carried out in a settling tank (9), and then clarified in a centrifuge (40) to produce treated water (5).
The method shown in FIG. In addition, ■ is returned sludge.
しかしながら、これらの方法には種々の問題点がある。However, these methods have various problems.
すなわち第１図の方法では、
■ 沈殿槽３０で分離された沈降性のよい汚泥には不活
性分が多く、汚泥重量当りの浄化効率が劣り、汚泥濃度
の増大に比例しだ浄化能力の増大が得られないこと
■ 沈殿槽３０からの溢流水の清澄化の装置として遠心
分離機４０を用いているため、その水量負荷を、通常の
汚泥処理工程で適用する水量負荷に比べて相当に小さく
しなければならず、従って単位処理水量当たりの動力消
費量が多大になることである。In other words, in the method shown in Fig. 1, ■ The sludge separated in the settling tank 30 with good settling properties has a large amount of inert content, and the purification efficiency per sludge weight is poor, and the purification capacity increases in proportion to the increase in the sludge concentration. ■ Since the centrifuge 40 is used as a device for clarifying the overflow water from the settling tank 30, the water load is considerably smaller than that applied in the normal sludge treatment process. Therefore, the amount of power consumed per unit amount of water to be treated becomes large.
また、第２図の方法においては、
■ 生物処理槽流出液の全量を遠心分離機４０にて固液
分離するため、原水の濃度変動に対応して汚泥の処理量
を円滑に加減するととが難しく維持管理が面倒であるこ
と
■ 遠心分離液中のＳＳ濃度を一定量以下に減少させる
と同時に生物処理槽内のＭＬＳＳ濃度を一定量に維持す
ることが難しく安定した処理を行うことが難しいことで
ある。In addition, in the method shown in Fig. 2, (1) Since the entire amount of the biological treatment tank effluent is separated into solid and liquid using the centrifuge 40, it is possible to smoothly adjust the amount of sludge treated in response to changes in the concentration of raw water. Difficult and troublesome to maintain and manage ■ It is difficult to reduce the SS concentration in the centrifuged liquid below a certain level and at the same time maintain the MLSS concentration in the biological treatment tank at a certain level, making it difficult to perform stable treatment. It is.
本発明け、これらの欠点を解消するための方法を提供す
ることを目的としたものである。It is an object of the present invention to provide a method for eliminating these drawbacks.
即ち本発明は、有機性汚水を第１脱窒素工程。That is, in the present invention, organic wastewater is subjected to the first denitrification step.
硝酸化工程、第２脱窒素工程、再曝気工程の順で処理す
る生物学的硝化脱窒素状において、前記第２脱窒素工程
流出液の一部を遠心濃縮工程で濃縮汚泥と分離液に分離
し、該遠心濃縮汚泥の一部を前記第１脱窒素工程へ返送
し残部を余剰汚泥とすると共に、前記流・出液の残部と
前記遠心分離液を再曝気工程及び固液分離工程に導いて
処理することを特徴とする高濃度有機性汚水の処理方法
である。In biological nitrification and denitrification, which is processed in the order of nitrification process, second denitrification process, and reaeration process, a part of the second denitrification process effluent is separated into thickened sludge and separated liquid in a centrifugal concentration process. Then, a part of the centrifugally concentrated sludge is returned to the first denitrification process and the remaining part is used as surplus sludge, and the remaining part of the flow/effluent and the centrifuged liquid are led to a re-aeration process and a solid-liquid separation process. This is a method for treating highly concentrated organic wastewater.
本発明の一実施態様を第３図に示すフローシートに従っ
て説明すると、
し銀系汚水などの高濃度の有機性汚水１は第１脱窒素槽
２に流入し、次の硝酸化槽３より循環されてきた硝化液
９と、更に遠心濃縮機５よりの濃縮返送汚泥１０と混合
処理され、脱窒素菌の働きにより硝化液９中の硝酸性窒
素及び亜硝酸性窒素を還元して窒素ガスにする。次に、
硝酸化槽３では、汚水中のアンモニア性窒素を硝化菌の
働きにより硝酸性窒素及び亜硝酸性窒素に硝化する。One embodiment of the present invention will be explained according to the flow sheet shown in FIG. The nitrified liquid 9 is further mixed with the concentrated return sludge 10 from the centrifugal concentrator 5, and the nitrate nitrogen and nitrite nitrogen in the nitrified liquid 9 are reduced to nitrogen gas by the action of denitrifying bacteria. do. next,
In the nitrification tank 3, ammonia nitrogen in the wastewater is nitrified into nitrate nitrogen and nitrite nitrogen by the action of nitrifying bacteria.
硝化液９の一部は次の第２脱窒素槽４に流入し、脱窒素
菌の働きによシ硝酸性窒素及び亜硝酸性窒素を窒素ガス
に還元する。A portion of the nitrifying solution 9 flows into the next second denitrification tank 4, where nitrate nitrogen and nitrite nitrogen are reduced to nitrogen gas by the action of denitrifying bacteria.
第２脱窒素槽４からの流出液の一部４ａは次の遠心濃縮
機５にかけて、その濃縮汚泥ダの一部を上記濃縮返送汚
泥１０として第１脱窒素槽２に返送し、分離液ダは次の
再曝気槽６に移送する。なお、１２は余剰汚泥である。A part of the effluent 4a from the second denitrification tank 4 is passed through the next centrifugal concentrator 5, and a part of the concentrated sludge is returned to the first denitrification tank 2 as the concentrated return sludge 10, and the separated liquid is returned to the first denitrification tank 2. is transferred to the next reaeration tank 6. Note that 12 is surplus sludge.
本発明は、第２脱窒素槽４からの流出液の一部４ａを遠
心濃縮機５にかけて、その濃縮汚泥５′の一部を返送汚
泥、残部を余剰汚泥とすることに特徴を有する。即ち、
■ 汚泥を遠心濃縮機５で濃縮し、その一部を余剰汚泥
として系外に取り出すので、後続する固液分離工程で沈
殿槽７から汚泥が上澄液（処理水８）と共に流出するこ
とを防止できるとと■ 第２脱窒素槽４内の活性ある汚
泥を強制的に濃縮し、それを第１脱窒素槽２への返送汚
泥とするので、汚泥重量当シの浄化効率を高めることが
できること
■ 第２脱窒素槽４からの流出液の一部４ａを遠心濃縮
機５で処理するので、原水の濃度変動に対して容易に対
処でき、生物処理槽のＭＬＳ Ｓ濃度を一定に維持する
ことができ安定した生物処理が可能であること
等の効果を得ることができる。The present invention is characterized in that a portion 4a of the effluent from the second denitrification tank 4 is passed through the centrifugal concentrator 5, and a portion of the concentrated sludge 5' is returned as sludge and the remainder is used as surplus sludge. That is, (1) The sludge is concentrated in the centrifugal thickener 5 and a part of it is taken out of the system as surplus sludge, so the sludge flows out from the settling tank 7 together with the supernatant liquid (treated water 8) in the subsequent solid-liquid separation process. ■ Active sludge in the second denitrification tank 4 is forcibly concentrated and returned to the first denitrification tank 2 as sludge, increasing the purification efficiency per sludge weight. ■ Since a part of the effluent 4a from the second denitrification tank 4 is treated with the centrifugal concentrator 5, fluctuations in the concentration of raw water can be easily dealt with, and the MLSS concentration in the biological treatment tank can be kept constant. It is possible to obtain effects such as being able to maintain stable biological treatment.
次に、第２脱窒素槽４からの流出液の残部４ｂは遠心濃
縮機５による上記分離液ダと共に再曝気槽６に移送し脱
気を行なう。分離液ダ中に・け通常微細な気泡が含有さ
れるので、後続する沈殿槽７における汚泥の浮上を防止
すると共に、＄２脱窒素処理で残留するＮＯ工を硝化す
る。Next, the remainder 4b of the effluent from the second denitrification tank 4 is transferred to the re-aeration tank 6 together with the liquid separated by the centrifugal concentrator 5 for deaeration. Since the separated liquid usually contains fine air bubbles, it prevents the sludge from floating in the subsequent settling tank 7, and nitrifies the NO gas remaining in the $2 denitrification process.
次に、再曝気処理液を沈殿槽７に流入させ、重力式沈降
分離法により汚泥の固液分離を行なう。Next, the reaeration treatment liquid is caused to flow into the settling tank 7, and solid-liquid separation of the sludge is performed by gravity sedimentation separation method.
従来の処理方法だと固液分離工程として機械的分離法を
使用せざるを得ないのであるが、本発明方法においては
前記のように、前段階で遠心濃縮機５により汚泥の一部
を余剰汚泥として系外に排出しているので、沈殿槽流入
混合液の汚泥濃度を１０００〜３０００ ’Ｉｆ／ｌ
Ｋ下げることができ、沈殿槽７での汚泥負荷を小さくす
ることができる。この結果、沈殿槽上澄液すなわち処理
水８の水質も向上し、処理の安定性本増加する。Conventional treatment methods have no choice but to use a mechanical separation method as a solid-liquid separation step, but in the method of the present invention, as mentioned above, a portion of the excess sludge is removed using the centrifugal thickener 5 in the previous stage. Since it is discharged outside the system as sludge, the sludge concentration of the mixed liquid flowing into the sedimentation tank should be set at 1000 to 3000 'If/l.
K can be lowered, and the sludge load in the settling tank 7 can be reduced. As a result, the quality of the sedimentation tank supernatant liquid, that is, the treated water 8, is also improved, and the stability of the treatment is increased.
なお、重力式沈殿槽７の代シに加圧浮上式分離装置を設
ける場合には、再曝気槽６のような脱気の必要はなく、
上記流出液４ｂと分離液ぎの単なる混合槽を設ければよ
い。なお、１１は余剰汚泥である。In addition, when a pressurized flotation type separator is provided in place of the gravity type settling tank 7, there is no need for deaeration as in the re-aeration tank 6.
A simple mixing tank for the above-mentioned effluent 4b and separation liquid may be provided. In addition, 11 is surplus sludge.
次に本発明の実施例を示す。Next, examples of the present invention will be shown.
実施例１゜
下記の水質を有する生し尿を第３図に示す生物学的硝化
脱窒素状によシ無希釈生物処理した。Example 1 Raw human waste having the following water quality was subjected to biological nitrification and denitrification as shown in FIG. 3 without dilution.
Ｂ ＯＤ １２０００〜２００００■μＮＨ
４−Ｎ ３０００〜５０００ ＃Ｃ’ＯＤ
Ｍ、 ５０００〜８０００ ＃２） 処理
プロセスの仕様 運転条件
第１脱窒素槽滞留時間 ３日
硝酸化種滞留時間 ５日
第２脱窒素槽滞留時間 １日
硝化液循環量 生し尿流入量の ３０倍遠心濃縮機処
理量 〃 の１．３倍濃縮汚泥返送量
〃 の０．５倍生物処理工程内ＭＬＳ８ １０００
０〜２ｏｏｏｏｑ／ｚ硝酸化槽内ＤＯレベル
１〜４ ｍｙＡ余 剰 汚 泥 量（２）
生し尿流入量の０．０５倍〃 （ロ） 〃
の０．４０倍第２脱嗜素槽からの流出液の１０〜２
０％を遠心濃縮機に供給し、遠心濃縮汚泥（ＳＳ濃度４
〜５チ）の８０〜９０チを第１脱窒素槽に返送した。第
２脱窒素槽流出液の残部と遠心製縮機分離液を再曝気槽
（滞留時間０，５〜１日）Ｋ流入せしめ充分曝気処理し
たのち、重力式沈殿槽（滞留時間１．５〜２日）に導入
して固液分離処理した。沈殿槽越流水の水質は下記のと
おりであり、無希釈処理水として良好なものであった。B OD 12000~20000μNH
4-N 3000~5000 #C'OD
M, 5000-8000 #2) Treatment process specifications Operating conditions First denitrification tank residence time 3 days Nitrated species residence time 5 days second denitrification tank residence time Nitrification liquid circulation amount per day 30 times the raw human waste inflow amount 1.3 times the centrifugal thickener processing capacity 〃 Thickened sludge return amount
〃 0.5 times biological treatment process MLS8 1000
0~2ooooq/z DO level in nitrification tank
1 to 4 myA surplus sludge amount (2)
0.05 times the amount of raw human urine inflow〃 (b)〃
0.40 times of the effluent from the second detoxication tank
0% to the centrifugal thickener, centrifugally thickened sludge (SS concentration 4
80 to 90 pieces of the sample (~5 pieces) were returned to the first denitrification tank. The remainder of the effluent from the second denitrification tank and the liquid separated from the centrifugal condensing machine are introduced into a re-aeration tank (residence time: 0.5 to 1 day) and sufficiently aerated. 2 days) and subjected to solid-liquid separation treatment. The water quality of the overflow water from the sedimentation tank was as shown below, and was good as non-diluted treated water.
３）沈殿槽越流水の水質
ＢＯＤ ２０〜６０岬Ａ
ＣＯＤＭｎ１００〜３００Ｉ
ＮＨ４，−Ｎ １０〜１５〃
Ｎ０ｊｃ−８２０〜５０ ｌｌ
５Ｓ ３０〜５０ 〃以上述べたよう
に、本発明によれば高濃度の有機性汚水を安定して、か
つ高い浄化効率で処理することができ、運転操作・維持
管理も極めて簡便に行なえるなどの効果が得られる。3) Water quality of settling tank overflow BOD 20-60 Cape A CODMn100-300I NH4,-N 10-15 N0jc-820-50 ll 5S 30-50 As described above, according to the present invention, high concentration Organic wastewater can be treated stably and with high purification efficiency, and operation and maintenance can be performed extremely easily.
第１図及び第２図は、いずれも従来方法の代表例を示す
フローシート、第３図は、本発明の一実施態様を示すフ
ローシートである。
１・−・有′機性汚水、２・−・第１脱窒素槽、３・・
・硝酸化槽、４・・−第２脱窒素槽、５・・・遠心濃縮
機、６・・・再曝気槽、７・・・沈殿槽、８・・・処理
水、９・・・硝化液、１０・・・濃縮返送汚泥、ｉｉ
、 １２・・・余剰汚泥。
特許出願人 荏原インフィルコ株式会社代理人弁理士
端 山 五 −
同 弁理士 千 １） 稔1 and 2 are flow sheets showing typical examples of conventional methods, and FIG. 3 is a flow sheet showing one embodiment of the present invention. 1.--Organic wastewater, 2.-.1st denitrification tank, 3.-.
・Nitrification tank, 4...-Second denitrification tank, 5...Centrifugal concentrator, 6...Reaeration tank, 7...Settling tank, 8...Treated water, 9...Nitrification Liquid, 10...Thickened return sludge, ii
, 12... Surplus sludge. Patent applicant: Patent attorney representing Ebara Infilco Co., Ltd.
Go Hayama - Patent attorney Sen 1) Minoru
Claims (1)
化脱窒素法において、 前記第２脱窒素工程流出液の一部を遠心濃縮工程で濃縮
汚泥と分離液に分離し、該遠心濃縮汚泥の一部を前記第
１脱窒素工程へ返送し残部を余剰汚泥とすると共に、前
記流出液の残部と前記遠心分離液を再曝気工程及び固液
分離工程に導いて処理することを特徴とする高濃度有機
性汚水の処理方法。 ２、前記固液分離工程が、前記再曝気工程の後段に設け
られ、重力式沈降分離法により行なわれるものである特
許請求の範囲第１項記載の方法。 ３、 前記再曝気工程及び固液分離工程が、加圧浮上分
離工程によシ並行して行なわれるものである特許請求の
範囲第１項記載の方法。[Claims] 1. Organic wastewater is subjected to a first denitrification process and a nitrification process. In the biological nitrification denitrification method in which the second denitrification step and the reaeration step are performed in this order, a part of the second denitrification step effluent is separated into thickened sludge and separated liquid in a centrifugal concentration step, and the centrifugation A part of the concentrated sludge is returned to the first denitrification process and the remaining part is used as surplus sludge, and the remaining part of the effluent and the centrifuged liquid are led to a re-aeration process and a solid-liquid separation process for treatment. A method for treating highly concentrated organic wastewater. 2. The method according to claim 1, wherein the solid-liquid separation step is provided after the reaeration step and is carried out by a gravity sedimentation separation method. 3. The method according to claim 1, wherein the reaeration step and the solid-liquid separation step are performed in parallel with a pressure flotation separation step.
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11399782A JPS596996A (en) | 1982-07-02 | 1982-07-02 | Treatment of organic filthy water of high concentration |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP11399782A JPS596996A (en) | 1982-07-02 | 1982-07-02 | Treatment of organic filthy water of high concentration |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS596996A true JPS596996A (en) | 1984-01-14 |
| JPS645959B2 JPS645959B2 (en) | 1989-02-01 |
Family
ID=14626469
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP11399782A Granted JPS596996A (en) | 1982-07-02 | 1982-07-02 | Treatment of organic filthy water of high concentration |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS596996A (en) |
Cited By (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59154197A (en) * | 1983-02-21 | 1984-09-03 | Showa Denko Kk | Biological denitrification method of organic waste |
| JPS60238199A (en) * | 1984-05-10 | 1985-11-27 | Kurita Water Ind Ltd | Method for keeping activity of sludge in biological nitration and denitrification treatment apparatus |
| JPS63142188A (en) * | 1986-12-01 | 1988-06-14 | 石川島播磨重工業株式会社 | Shield excavator |
| JPS6422400A (en) * | 1987-07-18 | 1989-01-25 | Kajima Corp | Waste water treatment |
| JPH0262997U (en) * | 1988-10-26 | 1990-05-10 |
-
1982
- 1982-07-02 JP JP11399782A patent/JPS596996A/en active Granted
Cited By (7)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS59154197A (en) * | 1983-02-21 | 1984-09-03 | Showa Denko Kk | Biological denitrification method of organic waste |
| JPS6322200B2 (en) * | 1983-02-21 | 1988-05-11 | Showa Denko Kk | |
| JPS60238199A (en) * | 1984-05-10 | 1985-11-27 | Kurita Water Ind Ltd | Method for keeping activity of sludge in biological nitration and denitrification treatment apparatus |
| JPS6333438B2 (en) * | 1984-05-10 | 1988-07-05 | Kurita Water Ind Ltd | |
| JPS63142188A (en) * | 1986-12-01 | 1988-06-14 | 石川島播磨重工業株式会社 | Shield excavator |
| JPS6422400A (en) * | 1987-07-18 | 1989-01-25 | Kajima Corp | Waste water treatment |
| JPH0262997U (en) * | 1988-10-26 | 1990-05-10 |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS645959B2 (en) | 1989-02-01 |
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