JPH0247278B2 - - Google Patents
Info
- Publication number
- JPH0247278B2 JPH0247278B2 JP57076937A JP7693782A JPH0247278B2 JP H0247278 B2 JPH0247278 B2 JP H0247278B2 JP 57076937 A JP57076937 A JP 57076937A JP 7693782 A JP7693782 A JP 7693782A JP H0247278 B2 JPH0247278 B2 JP H0247278B2
- Authority
- JP
- Japan
- Prior art keywords
- tank
- denitrification
- bod
- sludge
- denitrification tank
- 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 - Lifetime
Links
- 239000010802 sludge Substances 0.000 claims description 26
- 239000007788 liquid Substances 0.000 claims description 16
- 239000002351 wastewater Substances 0.000 claims description 14
- 238000000034 method Methods 0.000 claims description 12
- 238000007664 blowing Methods 0.000 claims description 5
- 238000013019 agitation Methods 0.000 claims description 3
- 239000012530 fluid Substances 0.000 claims description 3
- 241000894006 Bacteria Species 0.000 description 13
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 12
- 239000007789 gas Substances 0.000 description 9
- 230000003647 oxidation Effects 0.000 description 8
- 238000007254 oxidation reaction Methods 0.000 description 8
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 description 7
- 230000001590 oxidative effect Effects 0.000 description 7
- 239000001301 oxygen Substances 0.000 description 7
- 229910052760 oxygen Inorganic materials 0.000 description 7
- 229910052757 nitrogen Inorganic materials 0.000 description 6
- 230000000694 effects Effects 0.000 description 5
- 238000004062 sedimentation Methods 0.000 description 5
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 4
- 238000003756 stirring Methods 0.000 description 4
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 description 4
- MYMOFIZGZYHOMD-UHFFFAOYSA-N Dioxygen Chemical compound O=O MYMOFIZGZYHOMD-UHFFFAOYSA-N 0.000 description 2
- 238000007796 conventional method Methods 0.000 description 2
- 230000002503 metabolic effect Effects 0.000 description 2
- 125000001477 organic nitrogen group Chemical group 0.000 description 2
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 1
- 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 1
- 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 1
- 238000005273 aeration Methods 0.000 description 1
- 230000007423 decrease Effects 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 230000001546 nitrifying effect Effects 0.000 description 1
- 238000006864 oxidative decomposition reaction Methods 0.000 description 1
- 230000036284 oxygen consumption Effects 0.000 description 1
- 238000004064 recycling Methods 0.000 description 1
- 230000000284 resting effect Effects 0.000 description 1
- 230000037351 starvation Effects 0.000 description 1
- 239000006228 supernatant Substances 0.000 description 1
- 239000000725 suspension Substances 0.000 description 1
- 238000004065 wastewater treatment Methods 0.000 description 1
Landscapes
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Description
【発明の詳細な説明】
本発明は、廃水の生物学的脱窒素法に関し、更
に詳しくは廃水中の有機態窒素及びアンモニア態
窒素の除去に特に顕著な効果を奏する生物学的脱
窒素法に関する。DETAILED DESCRIPTION OF THE INVENTION The present invention relates to a biological denitrification method for wastewater, and more particularly to a biological denitrification method that is particularly effective in removing organic nitrogen and ammonia nitrogen from wastewater. .
有機態窒素及びアンモニア態窒素（以下これ等
を窒素成分と総称する）の除去を目的として脱窒
槽、BOD酸化槽（或いは硝化槽）及び沈降槽を
使用する廃水の活性汚泥処理法は、公知である。
しかしながら、公知の方法においては、脱窒槽の
撹拌を機械的手段で行なう為動力費が高価とな
る、機械的撹拌では汚泥フロツクの微細化が十分
に行なわれない為処理効率が低い、従つて脱窒率
を十分に高める為には複数個の脱窒槽を使用する
必要がある等の種々の難点が存在する。 The activated sludge treatment method for wastewater that uses a denitrification tank, a BOD oxidation tank (or nitrification tank), and a settling tank for the purpose of removing organic nitrogen and ammonia nitrogen (hereinafter collectively referred to as nitrogen components) is a known method. be.
However, in known methods, the denitrification tank is agitated by mechanical means, resulting in high power costs, and mechanical agitation does not sufficiently refine the sludge flocs, resulting in low treatment efficiency. There are various disadvantages such as the need to use a plurality of denitrification tanks in order to sufficiently increase the nitrification rate.
本発明者は、脱窒槽、BOD酸化槽及び沈降槽
を使用する公知の廃水の生物学的脱窒素法の問題
点に留意しつつ研究を重ねた結果、脱窒槽内の諸
条件を特定範囲内に保持し且つ脱窒槽内の液撹拌
を空気吹込みにより行なう場合には、動力費が大
巾に節減され、汚泥フロツクの微細化により脱
窒、BOD酸化等の処理効率が大巾に向上し、
BOD酸化槽の小型化が可能となり、BOD酸化槽
への曝気用空気又は酸素吹込み量が減少する等の
顕著な効果が奏されることを見出した。 As a result of repeated research while paying attention to the problems of known biological denitrification methods for wastewater that use a denitrification tank, a BOD oxidation tank, and a settling tank, the inventor has determined that the various conditions inside the denitrification tank are within a specific range. If the liquid is kept at a constant temperature and the liquid in the denitrification tank is stirred by air blowing, the power cost will be greatly reduced, and the processing efficiency of denitrification, BOD oxidation, etc. will be greatly improved by making the sludge flocs finer. ,
It has been found that the BOD oxidation tank can be downsized and the amount of aeration air or oxygen blown into the BOD oxidation tank can be reduced, resulting in significant effects.
すなわち、本発明は、下記の方法を提供するも
のである：
脱窒槽、硝化槽及び沈降槽を順次使用する廃水
の生物学的脱窒素法において、
() 開放型の脱窒槽内の撹拌を空気吹き込みに
より行ない、
() 被処理廃水、密閉型の硝化槽からの循環液
及び沈降槽から返送汚泥により形成される脱窒
槽内汚泥濃度を2000〜8000mg／の範囲内に保
持し、
() 脱窒槽内のBOD濃度を25ppm以上とし、
() 脱窒槽内への空気吹込み量を空気量／脱窒
槽内液量＝0.5〜10m3／m3・hrの範囲内に保持
する
ことを特徴とする廃水の生物学的脱窒素法。 That is, the present invention provides the following method: In a biological denitrification method for wastewater that sequentially uses a denitrification tank, a nitrification tank, and a sedimentation tank, () agitation in an open denitrification tank is replaced with air; () The sludge concentration in the denitrification tank formed by the wastewater to be treated, the circulating liquid from the closed nitrification tank, and the sludge returned from the settling tank is maintained within the range of 2000 to 8000 mg/, () The denitrification tank () The amount of air blown into the denitrification tank is maintained within the range of air amount/liquid amount in the denitrification tank = 0.5 to 10 m 3 /m 3 hr. Biological denitrification of wastewater.
周知の如く、好気性条件下にある硝化槽中には
BOD酸化菌、亜硝酸菌及び硝化菌が生息してお
り、廃水中の窒素成分を順次NH+ 4、NO- 2及び
NO- 3に酸化して行く。そして、脱窒槽内に生息
する通性嫌気性菌即ち脱窒菌によりNO- 2及び
NO- 3が最終的にN2に還元され、大気中に放散さ
れる。一般に、脱窒槽においては、溶存酸素濃度
（DO）0.5ppm以下の嫌気性状態において脱窒菌
がNO- 2及びNO- 3を体内に取り入れ、これ等をN2
に転換させるものと考えられている。即ち、DO
が0.5ppmを上回る好気性状態においては、脱窒
菌は、BOD酸化菌としての代謝活動を行ない、
BODの酸化処理を行なうのである。従つて、脱
窒槽に空気を吹込んで汚泥の撹拌を行なうことは
DO濃度を増大させて脱窒菌としての活動を阻害
し、BOD酸化菌としての活動を活発化させる為、
従来常識からは到底考え難いところであつた。し
かるに、本発明者の研究によれば、脱窒槽内の
BOD濃度を25ppm以上とし、脱窒槽内のMLSS
を2000〜8000mg／に保持しつつ、特定条件下に
空気吹込みを行なう場合には、BOD酸化菌の酸
素消費速度によつて脱窒槽内のDOは0.5ppm以下
に維持され、脱窒菌が活発に代謝活動を行ない、
極めて良好な窒素除去効果が達成されるのであ
る。 As is well known, in a nitrification tank under aerobic conditions,
BOD oxidizing bacteria, nitrite bacteria, and nitrifying bacteria live there, and they sequentially convert nitrogen components in wastewater into NH + 4 , NO - 2 , and
It oxidizes to NO - 3 . Then, NO - 2 and
NO - 3 is eventually reduced to N2 and dissipated into the atmosphere. Generally, in a denitrification tank, denitrifying bacteria take NO - 2 and NO - 3 into the body under anaerobic conditions with a dissolved oxygen concentration (DO) of 0.5 ppm or less, and convert these into N 2
It is thought that it will convert to That is, D.O.
In aerobic conditions where BOD exceeds 0.5 ppm, denitrifying bacteria perform metabolic activities as BOD oxidizing bacteria.
This involves oxidizing BOD. Therefore, it is not possible to stir the sludge by blowing air into the denitrification tank.
In order to increase DO concentration, inhibit the activity of denitrifying bacteria, and activate the activity of BOD oxidizing bacteria,
This was completely inconceivable based on conventional wisdom. However, according to the research of the present inventor, the denitrification tank
MLSS in the denitrification tank with a BOD concentration of 25ppm or more
If air is blown under specific conditions while maintaining DO at 2000 to 8000mg/, the oxygen consumption rate of BOD oxidizing bacteria will keep DO in the denitrification tank below 0.5ppm, and denitrification bacteria will become active. carry out metabolic activities,
A very good nitrogen removal effect is achieved.
以下本発明の一実施態様を示すフローチヤート
を参照しつつ、本発明をより詳細に説明する。 The present invention will be described in more detail below with reference to a flowchart showing one embodiment of the present invention.
処理さるべき廃水は、ライン１を経て脱窒槽３
に供給される。脱窒槽３には、硝化槽即ちBOD
酸化槽）５からの循環液がライン７を経て、又沈
降槽９からの返送汚泥がライン１１を経て、夫々
送給されており、そのBOD濃度は25ppm以上に
保持されている。リサイクル比即ち循環液流量＋
返送汚泥流量／被処理水流量は、通常３〜15程度
である。脱窒槽３には、汚泥の撹拌を行なう為
に、ライン１３、ブロワー１５及びライン１７を
通つて空気（以下単に気体という場合がある）が
吹き込まれる。気体吹込みは、スパージヤ、散気
管、エゼクター等により行なわれる。１時間当り
脱窒槽内液１m2当りの空気吹込み量は、0.5〜10
m2の範囲内とする。脱窒槽３内では、硝化槽５か
らの循環液に含まれているDO及び吹込み空気に
より部分的に好気状態となる。しかしながらこの
状態で沈降槽９からの返送汚泥（いわゆる飢餓性
汚泥）が25ppm以上の高いBOD濃度の脱窒槽３
内の液と接触すると、脱窒槽３内の細菌の一部が
BOD酸化菌として働き、DOを高速度で消費する
ので、結局、脱窒槽３内のDOな0.5ppm以下とな
り、嫌気状態に保持されることになる。脱窒槽３
内のBOD濃度が25ppm未満では、DOが十分に消
費されず、嫌気状態に保持し得ない。又、空気吹
込み量が、脱窒槽内液１m3及び１時間当り0.5m3
未満では、脱窒槽３の懸濁汚泥が浮遊せず、槽底
に蓄積するのに対し、10m3を上回る場合には、
DOが0.5ppmを上回り、いずれの場合にも窒素除
去率が低下する。 Wastewater to be treated passes through line 1 to denitrification tank 3.
is supplied to Denitrification tank 3 includes a nitrification tank, or BOD.
The circulating liquid from the oxidation tank 5 is sent through line 7, and the return sludge from the settling tank 9 is sent through line 11, and the BOD concentration thereof is maintained at 25 ppm or higher. Recycling ratio, i.e. circulating fluid flow rate +
The return sludge flow rate/to-be-treated water flow rate is usually about 3 to 15. Air (hereinafter simply referred to as gas) is blown into the denitrification tank 3 through a line 13, a blower 15, and a line 17 in order to stir the sludge. Gas blowing is performed using a spargeer, a diffuser pipe, an ejector, or the like. The amount of air blown per 1 m2 of liquid in the denitrification tank per hour is 0.5 to 10
Within the range of m2 . Inside the denitrification tank 3, the DO contained in the circulating fluid from the nitrification tank 5 and the blown air create a partially aerobic state. However, in this state, the return sludge (so-called starvation sludge) from the settling tank 9 has a high BOD concentration of 25 ppm or more in the denitrification tank 3.
When it comes into contact with the liquid in the tank, some of the bacteria in the denitrification tank 3
Since it acts as a BOD oxidizing bacterium and consumes DO at a high rate, the DO in the denitrification tank 3 ends up being less than 0.5 ppm and is kept in an anaerobic state. Denitrification tank 3
If the BOD concentration in the reactor is less than 25 ppm, DO will not be sufficiently consumed and cannot be maintained in an anaerobic state. In addition, the amount of air blown is 0.5 m 3 per 1 m 3 of the liquid in the denitrification tank and 0.5 m 3 per hour.
If it is less than 10m3, the suspended sludge in denitrification tank 3 will not float and will accumulate at the bottom of the tank, but if it is more than 10m3 ,
When DO exceeds 0.5 ppm, the nitrogen removal rate decreases in both cases.
脱窒槽３を出る液は、ライン１８を経て硝化槽
５に送られる。硝化槽５内に於いては、ライン１
９から槽内上方空間に供給給される空気又は残素
富化空気、純酸素等の酸素含有気体が、ブロワー
２１、ライン２３及び散気管２５を経て、液内に
吹込まれる。硝化槽５内のMLSSは2000〜8000
mg／の範囲内とし、BOD汚泥負荷は、0.1〜１
Kg・BOD／Kg−SS・dayとする。MLSSが2000
mg／未満の場合には、汚泥濃度が低い為、脱窒
及びBODの酸化分解が十分に行なわれ難いのに
対し、8000mg／を上回ると、汚泥濃度が高い
為、懸濁を均一に保持し得ず、槽底に汚泥の一部
が沈殿する傾向がある。又、DOは2ppm以上の
好気条件とし、通常２〜6ppm程度とすることが
好ましい。尚、ライン２７からは排ガスが系外に
排出される。本発明方法に於ては、前述の如く、
撹拌気体として空気又は酸素含有気体を使用する
場合には脱窒槽３内ですでにBOD酸化が一部行
なわれているので、硝化槽５の容積を減少し得る
とともに、硝化槽５への酸素含有気体の吹込み量
を減少させることも出来る。 The liquid leaving the denitrification tank 3 is sent to the nitrification tank 5 via line 18. In the nitrification tank 5, line 1
Air, residue-enriched air, pure oxygen, or other oxygen-containing gas supplied from 9 to the upper space inside the tank is blown into the liquid through the blower 21, line 23, and diffuser pipe 25. MLSS in nitrification tank 5 is 2000 to 8000
mg/, and the BOD sludge load is 0.1 to 1.
Kg・BOD/Kg−SS・day. MLSS is 2000
If it is less than 8000mg/, the sludge concentration is low, making it difficult for denitrification and oxidative decomposition of BOD to occur sufficiently, whereas if it exceeds 8000mg/, the sludge concentration is high, making it difficult to maintain a uniform suspension. There is a tendency for some of the sludge to settle at the bottom of the tank. Further, the DO is preferably set to aerobic conditions of 2 ppm or more, and usually about 2 to 6 ppm. Note that exhaust gas is discharged from the line 27 to the outside of the system. In the method of the present invention, as mentioned above,
When air or an oxygen-containing gas is used as the stirring gas, since some BOD oxidation has already taken place in the denitrification tank 3, the volume of the nitrification tank 5 can be reduced, and the oxygen content in the nitrification tank 5 can be reduced. It is also possible to reduce the amount of gas blown.
硝化槽５内での処理を終えた液は、ライン２９
から沈降槽９に送られ、常法に従つて沈降処理を
受ける。上澄水は、ライン３１から系外に排出さ
れ、必要ならば、更に高次の処理を行なう。沈降
した汚泥の大部分は、沈降槽９からライン１１を
経て脱窒槽３に返送され、少量の余剰汚泥がライ
ン３３から系外に排出される。 The liquid that has been processed in the nitrification tank 5 is transferred to the line 29.
From there, it is sent to a sedimentation tank 9, where it undergoes sedimentation treatment in accordance with conventional methods. The supernatant water is discharged from the system through line 31, and is subjected to higher-level treatment if necessary. Most of the settled sludge is returned from the settling tank 9 to the denitrification tank 3 via the line 11, and a small amount of excess sludge is discharged from the system through the line 33.
本発明によれば、以下の如き顕著な効果が達成
される。 According to the present invention, the following remarkable effects are achieved.
() 脱窒槽の撹拌を機械的手段で行なう場合に
比して、動力費が低減される。() Power costs are reduced compared to when the denitrification tank is stirred by mechanical means.
() 脱窒槽の撹拌を機械的手段で行なう場合に
比して、汚泥フロツクの微細化が十分に行なわ
れるので、窒素除去効率が高い。() Compared to the case where the denitrification tank is agitated by mechanical means, the sludge flocs are sufficiently refined, so the nitrogen removal efficiency is high.
() 脱窒槽内にBOD酸化菌の休止領域を含む従
来法と異なり、脱窒槽内においてもBOD酸化
の一部を行ない得るので、後続する硝化槽の
BOD負荷を低下させ得る。従つて、硝化槽を
小型化し、且つ硝化槽における酸素供給量を減
少させることが出来る。() Unlike the conventional method, which includes a resting area for BOD oxidizing bacteria in the denitrification tank, part of the BOD oxidation can also be performed in the denitrification tank, so the subsequent nitrification tank is
Can reduce BOD load. Therefore, the nitrification tank can be downsized and the amount of oxygen supplied to the nitrification tank can be reduced.
実施例 １
第１図に示す形式の廃水処理装置を使用して廃
水を処理した。Example 1 Wastewater was treated using a wastewater treatment apparatus of the type shown in FIG.
縦0.3ｍ×横0.4ｍ×高さ0.4ｍの脱窒槽３に
DO5ppm、BOD濃度150ppm、アンモニア態窒素
濃度20ppmの廃水15／hrを供給し、これに硝化
槽５からのDO5ppmの循環液65／hr及び沈降
槽９からの返送汚泥10／hrを加え、脱窒槽１m3
当り毎時1.3Nm3の空気を吹込んだ。尚、脱窒槽
３及び硝化槽５内の懸濁汚泥濃度は、3500mg／
であつた。 Denitrification tank 3 with length 0.3m x width 0.4m x height 0.4m
15/hr of wastewater with DO5ppm, BOD concentration 150ppm, and ammonia nitrogen concentration 20ppm is supplied, to which 65/hr of DO5ppm circulating liquid from nitrification tank 5 and 10/hr of return sludge from sedimentation tank 9 are added to the denitrification tank. 1m3
1.3Nm3 of air was blown per hour. The suspended sludge concentration in the denitrification tank 3 and nitrification tank 5 is 3500mg/
It was hot.
次いで、脱窒槽３からの液を硝化槽５に送り、
ライン１９から純酸素15／hrを供給してDOを
5ppmに保つた。硝化槽５の大きさは縦0.2ｍ×横
0.8ｍ×高さ0.4ｍである。 Next, the liquid from the denitrification tank 3 is sent to the nitrification tank 5,
Supply pure oxygen 15/hr from line 19 to generate DO.
It was kept at 5ppm. The size of the nitrification tank 5 is 0.2m in length x width.
It is 0.8m x height 0.4m.
次いで、硝化槽５からの液を沈降槽９に送り、
汚泥と処理済水とに分離した。 Next, the liquid from the nitrification tank 5 is sent to the settling tank 9,
Separated into sludge and treated water.
処理済水中のアンモニア態窒素濃度は2ppm、
硝酸態窒素濃度は4ppm、亜硝酸態窒素は検出さ
れなかつた。又、BODは12ppmであつた。窒素
除去率は70％であり、BOD除去率は92％であつ
た。 Ammonia nitrogen concentration in treated water is 2ppm,
Nitrate nitrogen concentration was 4 ppm, and nitrite nitrogen was not detected. Also, BOD was 12ppm. The nitrogen removal rate was 70% and the BOD removal rate was 92%.
第１図は、本発明方法の一実施態様を示すフロ
ーチヤートである。
３……脱窒槽、５……硝化槽、７……循環液供
給ライン、９……沈降槽、１１……返送汚泥供給
ライン、１５……ブロワー、１７……撹拌用気体
吹込みライン、１９……空気又は酸素含有気体供
給ライン、２１……ブロワー、２５……散気管、
３３……余剰汚泥排出ライン。
FIG. 1 is a flowchart showing one embodiment of the method of the present invention. 3... Denitrification tank, 5... Nitrification tank, 7... Circulating liquid supply line, 9... Sedimentation tank, 11... Return sludge supply line, 15... Blower, 17... Stirring gas blowing line, 19 ... Air or oxygen-containing gas supply line, 21 ... Blower, 25 ... Diffuser pipe,
33... Surplus sludge discharge line.
Claims (1)
水の生物学的脱窒素法において、 () 開放型の脱窒槽内の撹拌を空気吹き込みに
より行ない、 () 被処理廃水、密閉型の硝化槽からの循環液
及び沈降槽からの返送汚泥により形成される脱
窒槽内汚泥濃度を2000〜8000mg／の範囲内に
保持し、 () 脱窒槽内のBOD濃度を25ppm以上とし、 () 脱窒槽内への空気吹込み量を空気量／脱窒
槽内液量＝0.5〜10m3／m3・hrの範囲内に保持
する ことを特徴とする廃水の生物学的脱窒素法。[Scope of Claims] 1. In a biological denitrification method for wastewater that sequentially uses a denitrification tank, a nitrification tank, and a settling tank, () agitation in an open denitrification tank is performed by blowing air; () wastewater to be treated; , The concentration of sludge in the denitrification tank, which is formed by the circulating fluid from the closed nitrification tank and the sludge returned from the settling tank, is maintained within the range of 2000 to 8000 mg/, () The BOD concentration in the denitrification tank is maintained at 25 ppm or more. () A biological denitrification method for wastewater characterized by maintaining the amount of air blown into the denitrification tank within the range of air amount/liquid amount in the denitrification tank = 0.5 to 10 m 3 /m 3 hr. .
Priority Applications (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7693782A JPS58193796A (en) | 1982-05-07 | 1982-05-07 | Biologically denitrifying method of waste water |
Applications Claiming Priority (1)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP7693782A JPS58193796A (en) | 1982-05-07 | 1982-05-07 | Biologically denitrifying method of waste water |
Publications (2)
| Publication Number | Publication Date |
|---|---|
| JPS58193796A JPS58193796A (en) | 1983-11-11 |
| JPH0247278B2 true JPH0247278B2 (en) | 1990-10-19 |
Family
ID=13619640
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| JP7693782A Granted JPS58193796A (en) | 1982-05-07 | 1982-05-07 | Biologically denitrifying method of waste water |
Country Status (1)
| Country | Link |
|---|---|
| JP (1) | JPS58193796A (en) |
Families Citing this family (3)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP4867097B2 (en) * | 2001-07-26 | 2012-02-01 | 栗田工業株式会社 | Biological denitrification method and biological denitrification apparatus |
| JP5597002B2 (en) * | 2010-03-19 | 2014-10-01 | 水ｉｎｇ株式会社 | Waste water treatment apparatus and waste water treatment method |
| JP5238830B2 (en) * | 2011-01-17 | 2013-07-17 | 株式会社東芝 | Waste water treatment equipment |
Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5738993A (en) * | 1980-08-22 | 1982-03-03 | Kubota Ltd | Denitrifying method for water treatment |
-
1982
- 1982-05-07 JP JP7693782A patent/JPS58193796A/en active Granted
Patent Citations (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JPS5738993A (en) * | 1980-08-22 | 1982-03-03 | Kubota Ltd | Denitrifying method for water treatment |
Also Published As
| Publication number | Publication date |
|---|---|
| JPS58193796A (en) | 1983-11-11 |
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