NO134045B - - Google Patents
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- NO134045B NO134045B NO2724/72A NO272472A NO134045B NO 134045 B NO134045 B NO 134045B NO 2724/72 A NO2724/72 A NO 2724/72A NO 272472 A NO272472 A NO 272472A NO 134045 B NO134045 B NO 134045B
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- sludge
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- water
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- 239000010802 sludge Substances 0.000 claims description 70
- 238000005273 aeration Methods 0.000 claims description 38
- 239000002351 wastewater Substances 0.000 claims description 33
- 238000000034 method Methods 0.000 claims description 28
- 238000004062 sedimentation Methods 0.000 claims description 28
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 21
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 claims description 19
- QVGXLLKOCUKJST-UHFFFAOYSA-N atomic oxygen Chemical compound [O] QVGXLLKOCUKJST-UHFFFAOYSA-N 0.000 claims description 17
- 239000001301 oxygen Substances 0.000 claims description 17
- 229910052760 oxygen Inorganic materials 0.000 claims description 17
- QGZKDVFQNNGYKY-UHFFFAOYSA-O Ammonium Chemical compound [NH4+] QGZKDVFQNNGYKY-UHFFFAOYSA-O 0.000 claims description 15
- 229910052757 nitrogen Inorganic materials 0.000 claims description 9
- 230000008569 process Effects 0.000 claims description 9
- 230000008021 deposition Effects 0.000 claims description 7
- 238000004176 ammonification Methods 0.000 claims description 6
- 239000000126 substance Substances 0.000 claims description 6
- 238000004065 wastewater treatment Methods 0.000 claims description 5
- 230000015556 catabolic process Effects 0.000 claims description 4
- 229910019142 PO4 Inorganic materials 0.000 claims description 3
- 230000008030 elimination Effects 0.000 claims description 3
- 238000003379 elimination reaction Methods 0.000 claims description 3
- 230000001546 nitrifying effect Effects 0.000 claims description 3
- 235000021317 phosphate Nutrition 0.000 claims description 3
- 150000003013 phosphoric acid derivatives Chemical class 0.000 claims description 3
- 239000010840 domestic wastewater Substances 0.000 claims description 2
- 239000008394 flocculating agent Substances 0.000 claims description 2
- 230000006872 improvement Effects 0.000 claims description 2
- 239000010842 industrial wastewater Substances 0.000 claims description 2
- 150000003868 ammonium compounds Chemical class 0.000 claims 1
- 239000010796 biological waste Substances 0.000 claims 1
- 230000015572 biosynthetic process Effects 0.000 claims 1
- 239000007788 liquid Substances 0.000 claims 1
- 150000002897 organic nitrogen compounds Chemical class 0.000 claims 1
- 230000001376 precipitating effect Effects 0.000 claims 1
- 239000008213 purified water Substances 0.000 claims 1
- 229910002651 NO3 Inorganic materials 0.000 description 14
- NHNBFGGVMKEFGY-UHFFFAOYSA-N Nitrate Chemical compound [O-][N+]([O-])=O NHNBFGGVMKEFGY-UHFFFAOYSA-N 0.000 description 13
- 230000002349 favourable effect Effects 0.000 description 11
- 241000196324 Embryophyta Species 0.000 description 9
- 241000894006 Bacteria Species 0.000 description 6
- MMDJDBSEMBIJBB-UHFFFAOYSA-N [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] Chemical class [O-][N+]([O-])=O.[O-][N+]([O-])=O.[O-][N+]([O-])=O.[NH6+3] MMDJDBSEMBIJBB-UHFFFAOYSA-N 0.000 description 4
- IOVCWXUNBOPUCH-UHFFFAOYSA-M Nitrite anion Chemical compound [O-]N=O IOVCWXUNBOPUCH-UHFFFAOYSA-M 0.000 description 3
- 241000605159 Nitrobacter Species 0.000 description 3
- 241000605122 Nitrosomonas Species 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- GQPLMRYTRLFLPF-UHFFFAOYSA-N Nitrous Oxide Chemical compound [O-][N+]#N GQPLMRYTRLFLPF-UHFFFAOYSA-N 0.000 description 2
- 229910052782 aluminium Inorganic materials 0.000 description 2
- XAGFODPZIPBFFR-UHFFFAOYSA-N aluminium Chemical compound [Al] XAGFODPZIPBFFR-UHFFFAOYSA-N 0.000 description 2
- XKMRRTOUMJRJIA-UHFFFAOYSA-N ammonia nh3 Chemical compound N.N XKMRRTOUMJRJIA-UHFFFAOYSA-N 0.000 description 2
- 230000008901 benefit Effects 0.000 description 2
- 239000012141 concentrate Substances 0.000 description 2
- 238000006731 degradation reaction Methods 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000003344 environmental pollutant Substances 0.000 description 2
- 239000007789 gas Substances 0.000 description 2
- 159000000014 iron salts Chemical class 0.000 description 2
- 238000002156 mixing Methods 0.000 description 2
- MWUXSHHQAYIFBG-UHFFFAOYSA-N nitrogen oxide Inorganic materials O=[N] MWUXSHHQAYIFBG-UHFFFAOYSA-N 0.000 description 2
- 231100000614 poison Toxicity 0.000 description 2
- 231100000719 pollutant Toxicity 0.000 description 2
- 238000001556 precipitation Methods 0.000 description 2
- 238000000746 purification Methods 0.000 description 2
- 230000008719 thickening Effects 0.000 description 2
- UMGDCJDMYOKAJW-UHFFFAOYSA-N thiourea Chemical class NC(N)=S UMGDCJDMYOKAJW-UHFFFAOYSA-N 0.000 description 2
- 239000003440 toxic substance Substances 0.000 description 2
- 229920003043 Cellulose fiber Polymers 0.000 description 1
- 241001465754 Metazoa Species 0.000 description 1
- 235000017517 Tephrosia purpurea Nutrition 0.000 description 1
- 240000004429 Tephrosia purpurea Species 0.000 description 1
- XSQUKJJJFZCRTK-UHFFFAOYSA-N Urea Natural products NC(N)=O XSQUKJJJFZCRTK-UHFFFAOYSA-N 0.000 description 1
- 230000000274 adsorptive effect Effects 0.000 description 1
- 125000000129 anionic group Chemical group 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 239000000440 bentonite Substances 0.000 description 1
- 229910000278 bentonite Inorganic materials 0.000 description 1
- SVPXDRXYRYOSEX-UHFFFAOYSA-N bentoquatam Chemical compound O.O=[Si]=O.O=[Al]O[Al]=O SVPXDRXYRYOSEX-UHFFFAOYSA-N 0.000 description 1
- 125000002091 cationic group Chemical group 0.000 description 1
- 238000006243 chemical reaction Methods 0.000 description 1
- 238000005352 clarification Methods 0.000 description 1
- 239000003651 drinking water Substances 0.000 description 1
- 235000020188 drinking water Nutrition 0.000 description 1
- 238000012851 eutrophication Methods 0.000 description 1
- 239000003337 fertilizer Substances 0.000 description 1
- 238000005189 flocculation Methods 0.000 description 1
- 230000016615 flocculation Effects 0.000 description 1
- 238000005188 flotation Methods 0.000 description 1
- 230000036541 health Effects 0.000 description 1
- 229910001385 heavy metal Chemical class 0.000 description 1
- 235000003642 hunger Nutrition 0.000 description 1
- 239000000852 hydrogen donor Substances 0.000 description 1
- 239000003112 inhibitor Substances 0.000 description 1
- 230000003993 interaction Effects 0.000 description 1
- 238000011835 investigation Methods 0.000 description 1
- 230000001788 irregular Effects 0.000 description 1
- 230000007246 mechanism Effects 0.000 description 1
- -1 nitrate ions Chemical class 0.000 description 1
- 150000002825 nitriles Chemical class 0.000 description 1
- 229910017464 nitrogen compound Inorganic materials 0.000 description 1
- 150000002830 nitrogen compounds Chemical class 0.000 description 1
- 239000001272 nitrous oxide Substances 0.000 description 1
- 239000002957 persistent organic pollutant Substances 0.000 description 1
- 150000002989 phenols Chemical class 0.000 description 1
- 230000001681 protective effect Effects 0.000 description 1
- 108090000623 proteins and genes Proteins 0.000 description 1
- 230000003134 recirculating effect Effects 0.000 description 1
- 230000000717 retained effect Effects 0.000 description 1
- 150000003839 salts Chemical class 0.000 description 1
- 239000013049 sediment Substances 0.000 description 1
- 239000007787 solid Substances 0.000 description 1
- 238000003756 stirring Methods 0.000 description 1
Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/1215—Combinations of activated sludge treatment with precipitation, flocculation, coagulation and separation of phosphates
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1205—Particular type of activated sludge processes
- C02F3/121—Multistep treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
-
- 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
Description
Nærværende oppfinnelse vedrorer en fremgangsmåte for å fjerne organisk og uorganisk bundet nitrogen fra avvann fra industri og husholdning. The present invention relates to a method for removing organic and inorganic bound nitrogen from wastewater from industry and households.
Det er kjent en fremgangsmåte for biologisk rensning av avvann etter den aktiverte slammetode, ved hvilken avbyggingen av forurensningene med bakterier på den ene side og A method is known for the biological treatment of waste water according to the activated sludge method, in which the degradation of the pollutants with bacteria on the one hand and
fjerningen av de voksende bakterier ved bakteriefortærende orga-nismer på den annen side gjennomføres i to fullstendig fra hverandre skilte trinn i rekkefolge. Herunder luftes det eventuelt på forhånd mekanisk klarete,til det forste trinn tilforte avvann under fremskaffelse av optimale livsbetingel- the removal of the growing bacteria by bacterivorous organisms, on the other hand, is carried out in two completely separate steps in sequence. Underneath, any previously mechanically clarified wastewater added to the first stage is aerated while providing optimal living conditions.
ser for bakteriene i en luftningsbeholder, hvorved oksygen-konsentrasjonen velges slik at det klårete avlop fra et til luftningsbeholderen etterkoblet; til det forste trinn horende avsetningsbekken, til hvilket awannet fores etter luftningen, etter en bestemt oppholdstid ikke lenger inneholder fritt oksygen. Oksygenfritt avvann, som tas ut fra dette avsetningsbekken, luftes nå igjen i det annet trinn i en luftningsbeholder slik, og slamkonsentrasjonen reguleres slik at avlopet fra en etter luftningsbeholderen i det annet trinn innkoblete og til dette annet trinn horende avsetningsbekken etter en bestemt oppholdstid oppviser et oksygeninnhold på minst 2 mg/l. looks for the bacteria in an aeration tank, whereby the oxygen concentration is chosen so that the clarified effluent from one to the aeration tank is connected afterwards; to the settling stream belonging to the first stage, to which the waste water is fed after the aeration, after a certain residence time no longer contains free oxygen. Oxygen-free wastewater, which is removed from this sedimentation stream, is now aerated again in the second stage in an aeration tank as follows, and the sludge concentration is regulated so that the effluent from a sedimentation stream connected after the aeration tank in the second stage and belonging to this second stage shows a oxygen content of at least 2 mg/l.
Ved avledningen av avvann i husholdning og industri til de naturlige vassdrag okes innholdet i disse på ammonium- og nitrat-nitrogenforbindelser konstant. Ammonium danner forsåvidt en fare for de naturlige vassdrag, da dette ved hoyere pH-verdier virker som fiskegifter eller ved inntredende nitrifikasjon kan fore til en oksygenmangel i vassdraget. Nitratet på sin side virker som gjodningsstoff og er en av årsakene til den tiltagende eutrofering av vassdragene. Det vanskeliggjør eller setter også i fare opparbeidelsen av disse vassdrag til drik-kevann, da nitrat i for hoy konsentrasjon kan fore til sunn-hetsmessige beskadigelser hos mennesker og dyr. Det hoye ammonium- og nitratinnhold i naturlige vassdrag er blant annet og-så å fore tilbake på den utilstrekkelig fjerning av disse stof-fer ved de vanlige, hittil kjente biologiske avvannsrensnings-metoder og anlegg og også ved den innledningsvis nevnte fremgangsmåte. When domestic and industrial waste water is diverted to natural waterways, the content of ammonium and nitrate-nitrogen compounds in these is constantly increased. Ammonium certainly poses a danger to natural watercourses, as at higher pH values this acts as fish poison or, when nitrification occurs, can lead to a lack of oxygen in the watercourse. Nitrate, on the other hand, acts as a fertilizer and is one of the reasons for the increasing eutrophication of watercourses. It also complicates or endangers the processing of these waterways into drinking water, as nitrate in too high a concentration can lead to health-related damage in humans and animals. The high ammonium and nitrate content in natural waterways is, among other things, to be traced back to the insufficient removal of these substances by the usual, hitherto known biological wastewater treatment methods and facilities and also by the method mentioned at the outset.
Det består derfor et sterkt behov for awannsrensningsmetoder og -anlegg som er i stand til å fjerne ammonium- og nitrationer såvel som organisk bundet nitrogen fra de tilforte avvann mest mulig. Forskjellige forslag går i retning av å nitrifisere ammoniumet i en aktivert slamprosess på i og for seg kjent må-te og denitrifisere det nitratholdige avvann i et spesielt etterinnkoblet trinn. Ved nitrifiseringen og denitrifiseringen må det tas hensyn til folgende: There is therefore a strong need for wastewater treatment methods and facilities that are able to remove ammonium and nitrate ions as well as organically bound nitrogen from the added wastewater as much as possible. Various proposals go in the direction of nitrifying the ammonium in an activated sludge process in a manner known per se and denitrifying the nitrate-containing wastewater in a special after-connected step. During nitrification and denitrification, the following must be taken into account:
Ved nitrifiseringen i et aktivert slamsystem oksyderes ammo-niumnitrogenet rnikrobielt til nitritt og nitrat. En stor del av det organisk bundne nitrogen, som ikke kan forbrukes ved inkarnering, omdannes ved ammonifiserende bakterier til ammo-niumnitrogen. Overforingen av ammonium til nitrat skjer ved nitrosomonas-bakterier, og omdannelsen av nitritt til nitrat ved nitrobacter. During nitrification in an activated sludge system, the ammonium nitrogen is oxidized microbially to nitrite and nitrate. A large part of the organically bound nitrogen, which cannot be consumed by incarnation, is converted by ammonifying bacteria into ammonium nitrogen. The transfer of ammonium to nitrate takes place by nitrosomonas bacteria, and the conversion of nitrite to nitrate by nitrobacter.
Det antas at veksthastigheten for nitrosomonas er mindre enn for nitrobacter, slik at de forstnevnte er en begrensende fak-tor for nitrifiseringen. Om en nitrifisering i et aktivert slamanlegg er mulig avhenger av forskjellige faktorer, blant annet av temperaturen, luftningstiden, slamkonsentrasjonen, slambelastningen, av nitrogeninnholdet og av inhibitorer såvel som av pH-verdien. It is assumed that the growth rate of nitrosomonas is less than that of nitrobacter, so that the former are a limiting factor for nitrification. Whether nitrification in an activated sludge plant is possible depends on various factors, including the temperature, the aeration time, the sludge concentration, the sludge load, the nitrogen content and inhibitors as well as the pH value.
En nitrifisering er da prinsipielt bare mulig når en viss slanw-belastning ved gitte temperaturer ikke overskrides. Ved slam-belastninger over 0,2 kg BOB5/kg STS (STS=slamtorrstoff) i tem-peraturområdet under 15°c inntrer ingen eller bare meget utilstrekkelig nitrifisering. Ved 20°c og slambelastning på inntil 0,33 kg B0B,-/kg STS kan en fullstendig nitrif isering oppnås. Nitrification is then in principle only possible when a certain slanw load at given temperatures is not exceeded. At sludge loads above 0.2 kg BOB5/kg STS (STS=sludge solids) in the temperature range below 15°c, no or only very insufficient nitrification occurs. At 20°c and a sludge load of up to 0.33 kg B0B/kg STS, complete nitrification can be achieved.
Nærværet av forskjellige giftige substanser i avvannet kan forhindrer en nitrifisering. Særlig hemmer tiokarbamid, cya-nider, fenoler og tungmetallsalter veksten av nitrifiserende bakterier. The presence of various toxic substances in the wastewater can prevent nitrification. In particular, thiourea, cyanides, phenols and heavy metal salts inhibit the growth of nitrifying bacteria.
Ved denitrifiseringen reduseres nitritt og nitrat til elemen-tært nitrogen og til dinitrogenoksyd. During denitrification, nitrite and nitrate are reduced to elemental nitrogen and nitrous oxide.
Mekanismen for denitrifiseringen er ennå ikke oppklart i alle henseender. Generelt oppfattes denne prosess som strengt anaerob prosess. Prinsipielt synes for denitrifiseringen hydrogen-donatorer nodvendige. Ved siden av oksygeninnholdets innfly-telse under denitrifiseringen spiller pH-verdien og oppholds-tiden en rolle. En vekselvirkning mellom pH-verdien og innfly-telsen av oksygenspenning ble fastslått for denitrifiserings-hastigheten. I pH-området >7 hemmes denitrifiseringen ved nærvær av oksygen. The mechanism of the denitrification has not yet been fully elucidated. In general, this process is perceived as a strictly anaerobic process. In principle, hydrogen donors seem necessary for denitrification. In addition to the influence of the oxygen content during denitrification, the pH value and residence time play a role. An interaction between the pH value and the influence of oxygen tension was established for the denitrification rate. In the pH range >7, denitrification is inhibited by the presence of oxygen.
Sammenfattende kan det fastslås at ved alle undersøkelser er sammenhengene mellom slamkonsentrasjon og tid såvel som tempe-ratur og slambelastning ved nitrifiseringen blitt erkjent. Likeledes ble det erkjent at en denitrifisering prinsipielt er mulig. In summary, it can be established that in all investigations the relationships between sludge concentration and time as well as temperature and sludge load during nitrification have been recognised. Likewise, it was recognized that denitrification is in principle possible.
Med utgang fra disse erkjennelser fremskaffer nærværende oppfinnelse en fremgangsmåte hvorved så og si samtidig med den vanlige rensning av avvann og uten nevneverdige ytterligere anstrengelser i tillegg til denne, kan det oppnås en utstrakt fjerning av ammonium-, nitrat- og organisk bundet nitrogen fra avvann fra husholdning og industri. Fremgangsmåten tar sikte på å skaffe mest mulig gunstige forutsetninger for alLle de viktige operasjoner. Based on these findings, the present invention provides a method by which, so to speak, simultaneously with the usual purification of waste water and without significant additional efforts in addition to this, an extensive removal of ammonium, nitrate and organically bound nitrogen from waste water can be achieved household and industry. The procedure aims to obtain the most favorable conditions possible for all the important operations.
Dette skjer i et biologisk avvannsrensningsanlegg av den i innledningen nevnte art, d.v.s. med to etter hverandre koblete trinn som hvert inneholder en luftningsbeholder og et etterkoblet avsetningsbekken, hvor avvannet i luftningsbeholderen i det forste trinn luftes og derpå fores til avsetning i forste trinns avsetningsbekken, fra hvilket det tas ut nitrogenfritt og fores til det annet trinn,hvor avvannet igjen luftes og derpå fores til avsetningsbekkenet i det annet trinn og karakteriseres ifolge oppfinnelsen ved at det fra avsetningsbekkenet. i det forste trinn uttatte ammoniumholdige, oksygenfrie avvann luftes i luftningsbeholderen for det annet trinn under fremskaffelse av gunstige betingelser for en mest mulig vidtgående nitrifisering av ammoniumet, og at en del av det på denne måte nitrif i serte avvann fra avsetningsbekkenet i det anne:t trinn kontinuerlig fores tilbake til det forste trinn og denitrifiseres 1 forste trinns avsetningsbekken, i hvilket gunstige betingelser frem-skaffes for ammonifiseringen av det organisk bundne nitrogen og for denitrifiseringen av det til avvannet tilforte og med det rensete avvann tilbakeforte nitrat°This takes place in a biological wastewater treatment plant of the type mentioned in the introduction, i.e. with two stages connected one after the other, each containing an aeration tank and a downstream settling stream, where the dewater in the aeration tank in the first stage is aerated and then fed to deposition in the first stage's settling stream, from which it is removed nitrogen-free and fed to the second stage, where the dewater again aerated and then fed to the settling basin in the second stage and characterized according to the invention by that from the settling basin. Ammonium-containing, oxygen-free wastewater removed in the first stage is aerated in the aeration tank for the second stage while providing favorable conditions for the most extensive nitrification of the ammonium possible, and that a part of the nitrif in this way in the wastewater from the settling basin in the other stage is continuously fed back to the first stage and denitrified 1 first stage sedimentation stream, in which favorable conditions are created for the ammonification of the organically bound nitrogen and for the denitrification of the nitrate added to the wastewater and returned with the purified wastewater°
Ved dette tas i det annet trinn ved meget lav BOB^-slambelast- In this case, in the second step at a very low BOB^-sludge load,
ning og hoy slamalder hensyn til den lille veksthastighet for Nit-robacter: og særlig Nitrosomonas. I avsetningsbekkenet i det forste trinn skaffes gunstige betingelser for denitrifiserin- ning and high sludge age due to the low growth rate of Nitrobacter: and especially Nitrosomonas. In the sedimentation basin in the first stage, favorable conditions are provided for denitrification
gen, hvorved den lave slambelastning med den derved betingete hoye slammengde i dette forste trinn samtidig gir en beskyttel- gene, whereby the low sludge load with the resulting high amount of sludge in this first stage simultaneously provides a protective
se for nitrif i ser ende bakterier i det annet trinn, idet toksisk virkende substanser for storstedelens vedkommende tilbakehol- look for nitrif in see ending bacteria in the second stage, as toxic substances for the most part are retained
des delvis adsorptivt i det forste trinn, delvis avbygges biologisk. Samtidig forsterkes den ammonifiserende virkning i det reduserende medium i avsetningsbekkenet. des partly adsorptive in the first step, partly degraded biologically. At the same time, the ammonifying effect of the reducing medium in the sedimentation basin is enhanced.
Ved dette oppnås innen anlegget en fjerning av det i det til anlegget tilforte avvann inneholdte totalnitrogen med inntil 90% uten forstyrrelse av avbyggingen av de ovrige forurens- This achieves within the plant a removal of up to 90% of the total nitrogen contained in the wastewater supplied to the plant without disturbing the degradation of the other pollutants.
ninger på den vanlige måte og under utnyttelse av de til en- nings in the usual way and under the utilization of the
hver tid for ammonifiseringen og nitrifiseringen henholdsvis denitrifiseringen gunstigste forutsetninger. each time for the ammonification and nitrification respectively denitrification most favorable conditions.
For å oke denne fjerning kan med fordel minst halvparten av To increase this removal, at least half of
det i avsetningsbekkenet i det annet trinn i lopet av 24 timer tilforte nitrifiserte avvann fra dette bekken igjen fores til det forste trinn og/eller det kan sorges for at omtrent like meget eller mer renset nitrifisert vann igjen kan ledes til det forste trinn som dette trinn samtidig i 24 timer tilfores urenset avvann for rensning. in the sedimentation basin in the second stage over the course of 24 hours added nitrified wastewater from this stream is again fed to the first stage and/or it can be ensured that roughly the same amount or more purified nitrified water can again be led to the first stage as this stage at the same time, for 24 hours, contaminated wastewater is supplied for purification.
Ved et anlegg med uregelmessig avvannstilforsel kan det med In the case of a facility with an irregular wastewater supply, it can also
fordel arbeides på den måte at anleggets hydrauliske belast- advantage is worked in such a way that the plant's hydraulic load
ning holdes konstant, innstilt på den forutsatte toppbelast-ning .Ved mindre avvannsbelastning kan videre så meget av det rensete nitrifiserte vann fores tilbake fra avsetningsbekkenet i det annet trinn til det forste trinn, at den hydrauliske belastning i det forste trinn forblir konstant. is kept constant, set to the assumed peak load. In the case of a smaller wastewater load, so much of the purified nitrified water can be fed back from the sedimentation basin in the second stage to the first stage, that the hydraulic load in the first stage remains constant.
Det fra avsetningsbekkenet i det annet trinn for denitrifiseringen i det forste trinn tilbakeforte vann kan enten ledes inn i luftningsbeholderen eller i avsetningsbekkenet i det forste trinn. En fordelaktig, særlig intim gjennomblanding av denne tilbakesirkulerende del med vannet i det forste trinn kan imidlertid oppnås ved at det tilbakeforte vann innfores i forbindelsesledningen mellom luftningsbeholderen og avsetningsbekkenet i det forste trinn. The water withdrawn from the sedimentation basin in the second stage for the denitrification in the first stage can either be led into the aeration tank or into the sedimentation basin in the first stage. An advantageous, particularly intimate mixing of this recirculating part with the water in the first stage can, however, be achieved by introducing the recirculated water into the connection line between the aeration container and the settling basin in the first stage.
For fremskaffelse av optimale betingelser for ammonifiseringen For obtaining optimal conditions for the ammonification
og denitrifiseringen i det forste trinn, når det arbeides med and the denitrification in the first stage, when working with
en 02-konsentrasjon på 0 - 2 mg 02/l og en slamkonsentrasjon på 5 - 15 kg STS/m<3>, kan fordelaktig BOBc-slambelastningen ligge mellom 0,5 - 0,05, fortrinnsvis ved 0,15 kg BOB5/kg slamtorrstoff, hvorved det stadig befinner seg minst 2/3 av det i det totale forste trinn tilstedeværende slam i avsetningsbekkenet i dette trinn. Slambelastningen regnes ut fra den pr. 24 timer i det forste trinn med avvannet tilflytende mengde i kg BOB^ dividert med den totale i det forste trinn inneholdte slammengde i kg. Slamalderen,som gir seg fra den i det totale forste trinn foreliggende slammengde, dividert med den daglig fra avvannet tiltagende eller tilforte slammengde i kg, kan være 5-30 dager, fortrinnsvis ca. 12 dager. Samtidig kan det-sorges foråt det til avsetningsbekkenet i det forste trinn tilforte slam gjennomgående etter minst en, hoyst imidlertid etter 8 timer, fortrinnsvis etter 3 timer, igjen kommer tilbake til den tilhorende luftningsbeholder og der forsynes med oksygen. Dette kan skje ved en tilsvarende dimensjonering av den an 02 concentration of 0 - 2 mg 02/l and a sludge concentration of 5 - 15 kg STS/m<3>, the BOBc sludge load can advantageously lie between 0.5 - 0.05, preferably at 0.15 kg BOB5/ kg of sludge dry matter, whereby at least 2/3 of the total sludge present in the first stage is still in the sedimentation basin in this stage. The sludge load is calculated from the 24 hours in the first stage with dewatered inflow quantity in kg BOB^ divided by the total quantity of sludge contained in the first stage in kg. The sludge age, which is obtained from the amount of sludge present in the total first stage, divided by the daily increasing or added amount of sludge in kg from dewatered, can be 5-30 days, preferably approx. 12 days. At the same time, it can be ensured that the sludge supplied to the sedimentation basin in the first stage is continuously supplied after at least one, but at most after 8 hours, preferably after 3 hours, again to the associated aeration tank and is supplied with oxygen there. This can be done by a corresponding dimensioning of it
tilbakeforte slammengde, f.eks. 1/5 til 1/2, fortrinnsvis 1/4 reclaimed sludge quantity, e.g. 1/5 to 1/2, preferably 1/4
åv avsetningsbekkeninnholdet pr. time. Da i lbpet av de-nitrif iseringsprosessen gassblærer oppstår i det indre: av slamflokkene flotterer en del av slammet til overflaten av bekkenet.' Dette slam kan på kjent måte skaves av og fores tilbake til of the sediment basin content per hour. Then in the lbpet of the de-nitrification process gas bubbles arise in the interior: of the sludge flocs, part of the sludge floats to the surface of the basin.' This sludge can be scraped off in a known manner and fed back to
den tilhorende luftningsbeholder eller trekkes av som over-skudds sl am. the associated aeration container or is drawn off as excess sludge.
Ved denne foranstaltning skaffes særlig gunstige betingelser This measure provides particularly favorable conditions
for ammonifiseringen og denitrifiseringen, da ved den hoye for the ammonification and denitrification, then at the high
oppholdstid for slammet i avsetningsbekkenet oksygenhungeren blir så stor at nitratet reduseres uten å påvirke fjerningen av biologisk avbyggbare organiske substanser. I motsetning fremmes denne fjerning ved den ytterligere nitrogentilførsel over nitratet, hvorved samtidig en energibesparelse er mulig, residence time for the sludge in the sedimentation basin, the oxygen hunger becomes so great that the nitrate is reduced without affecting the removal of biologically degradable organic substances. In contrast, this removal is promoted by the additional nitrogen supply above the nitrate, whereby at the same time an energy saving is possible,
da oksygentilførselen til luftningen i det forste trinn kan reduseres. as the oxygen supply to the aeration in the first stage can be reduced.
For fremskaffelse av gunstige forutsetninger for nitrifiseringen i det annet trinn, når det arbeides med oksygenkonsentra-sjoner på 2 - 6 mg 09/l og en slamkonsentrasjon på 0,5 - 4 kg STS/m , kan BOB^-slambelastningen vidtgående avhengig av temperaturen utgjore 0,3 - 0,01, fortrinnsvis 0,1 kg BOB^/kg slamtorrstoff. Slamalderen kan utgjore 5 - 30 dager, fortrinnsvis 12 dager. Samtidig kan det sorges for at til avsetningsbekkenet tilfort slam etter 1/4 time, senest etter 4 timer, fortrinnsvis etter 1 time, igjen kommer til den tilhorende luftningsbeholder og der forsynes med oksygen. Med fordel befinner stadig hoyst halvparten av det i det totale annet trinn foreliggende slam seg i tilhorende avsetningsbekken. Den tilbake-blivende slammengde reguleres f.eks. med fordel slik at den pr. time utgjor 1/5 - 1/2, fortrinnsvis 1/4, av avsetningsbekkenvolumet. To provide favorable conditions for the nitrification in the second stage, when working with oxygen concentrations of 2 - 6 mg 09/l and a sludge concentration of 0.5 - 4 kg STS/m , the BOB^ sludge load can vary greatly depending on the temperature constitute 0.3 - 0.01, preferably 0.1 kg BOB^/kg sludge dry matter. The sludge age can be 5 - 30 days, preferably 12 days. At the same time, it can be ensured that the sludge supplied to the sedimentation basin after 1/4 hour, at the latest after 4 hours, preferably after 1 hour, returns to the associated aeration tank and is supplied with oxygen there. Advantageously, at most half of the total sludge present in the second stage is always found in the associated deposition stream. The residual amount of sludge is regulated, e.g. with advantage so that it per hour constitutes 1/5 - 1/2, preferably 1/4, of the deposition basin volume.
Ved disse foranstaltninger skaffes særlig gunstige betingelser for nitrifiseringen, særlig ved den lave BOB^-slambelastning, ved det i det forste trinn allerede langtgående forrensete avvann og den derved oppnålige hoye slamalder. Spesielt unngås ved dette at i avsetningsbekkenet i det annet trinn Opptrer denitrifiseringstilfelle som forer til den kjente slamdrift som påvirker nitrifiseringen og gjor avlbpskvaliteten dårligere. With these measures, particularly favorable conditions for nitrification are obtained, especially with the low BOB^ sludge load, with the already extensive pre-purified wastewater in the first stage and the thereby attainable high sludge age. In particular, this avoids the occurrence of denitrification in the sedimentation basin in the second stage, which leads to the well-known sludge drift which affects nitrification and makes the quality of the product worse.
Det ble videre funnet at ved siden av avbyggingen av de organiske forurensninger og fjerningen av nitratnitrogenet og uten påvirkning av disse prosesser kan dessuten fosfater som foreligger i avvannet, som skal renses, elimineres. Dette kan skje ved at det i det annet trinn foran avsetningsbekkenet tilsettes i og for seg kjente fellingskjemikalier, f.eks. aluminium- eller jernsalter. It was further found that in addition to the breakdown of the organic pollutants and the removal of the nitrate nitrogen and without the influence of these processes, phosphates present in the wastewater, which is to be purified, can also be eliminated. This can be done by adding, in the second step, in front of the settling basin, precipitation chemicals known in and of themselves, e.g. aluminum or iron salts.
Oppfinnelsen forklares nærmere i det folgende med henvisning til den på tegningen som eksempel skjematisk gjengitte utfo-relsesform for et anlegg for gjennomføring av fremgangsmåten ifolge oppfinnelsen. The invention is explained in more detail in the following with reference to the embodiment shown schematically in the drawing as an example for a plant for carrying out the method according to the invention.
Tegningen viser et i og for seg kjent to-trinns biologisk avvannsrensningsanlegg med en forste luftningsbeholder 1 og et over en ledning 2 etterkoblet avsetningsbekken 3, som tilsam-men danner anleggets forste trinn. Over et overlop 4 og en The drawing shows a known in and of itself two-stage biological wastewater treatment plant with a first aeration tank 1 and a sedimentation stream 3 connected via a line 2, which together form the plant's first stage. Over an overlap 4 and one
ledning 5 er avsetningsbekkenet 3 i det forste trinn forbundet med en annen luftningsbeholder 6, som sammen med et ytterligere avsetningsbekken 7, som over en ledning 8 er forbundet med den annen luftningsbeholder 6 henholdsvis etterkoblet denne, danner det gjengitte anleggs annet trinn. Luftningen i luft-ningsbeholderne 1 og 6 skjer over egnete utstromningsanDrclninger 9 henh. 10, som er tilkoblet en felles tilforselslednincf 11. line 5, the sedimentation basin 3 in the first stage is connected to another aeration tank 6, which together with a further sedimentation basin 7, which is connected via a line 8 to the second aeration tank 6 or subsequently connected to this, forms the second stage of the reproduced plant. The aeration in the aeration containers 1 and 6 takes place via suitable outflow devices 9 acc. 10, which is connected to a common supply line 11.
Avvannet fra husholdning eller industri som skal renses og befris for ammonium og nitratnitrogen kommer, klaret på forhånd eller ikke, over en ledning 12 kontinuerlig inn i luft-ningsbekkenet 1 i det forste trinn og går derpå av gjennom ledningen 2 til det tilhorende etterkoblete avsetningstrinn med etterklaringsbekkenet 3. I dette forste fremgangsmåtetrinn i The waste water from households or industry that is to be cleaned and freed of ammonium and nitrate nitrogen comes, pre-clarified or not, via a line 12 continuously into the aeration basin 1 in the first stage and then leaves through the line 2 to the corresponding downstream deposition stage with the post-clarification basin 3. In this first procedure step i
avstemmes på i og for seg kj ent måte luftningstiden med luE t over ledningen 11 og utstromningsanordningen 9 innfort oksy-genmengde og konsentrasjonen av det biologiske slam slik at det klarete avlop gjennom ledningen 5 i dette forste avsetningstrinn ikke mere inneholder noe fritt oksygen i avsetningsbekkenet 3. BOBj--slambelastningen, basert på den totale slammengde i luftningsbeholderen 1 og avsetningsbekkenet 3 er 0,15 kg BOBg pr. kg slamtorrstoff. En tredjedel av denne totale the aeration time with the luE t over the line 11 and the outflow device 9 are adjusted in a known manner, the amount of oxygen and the concentration of the biological sludge are adjusted so that the clarified effluent through the line 5 in this first settling stage no longer contains any free oxygen in the settling basin 3 The BOBj sludge load, based on the total amount of sludge in the aeration tank 1 and the settling basin 3, is 0.15 kg BOBg per kg sludge dry matter. A third of this total
mengde befinner seg i luftningsbeholderen 1, to tredjedel i avsetningsbekkenet 3. Gjennom slamtilbakeforingsledningen 13 amount is in the aeration tank 1, two-thirds in the sedimentation basin 3. Through the sludge return line 13
pumpes så meget slam tilbake til luftningsbeholderen at denne \ mengde tilsvarer en fjerdedel av avsetningsbekkeninnholdet pr. i time. Det ovenpå svommende slam som samler seg på vannoverfla-ten i bekkenet 3 holdes tilbake av en neddykket vegg 18 og fores tilbake igjen med en egnet anordning over en ledning 19 so much sludge is pumped back to the aeration tank that this \ amount corresponds to a quarter of the sedimentation pond contents per per hour. The floating sludge that accumulates on the surface of the water in the basin 3 is held back by a submerged wall 18 and fed back again with a suitable device over a line 19
til luftningsbeholderen 1. På denne måte skaffes gunstige betingelser for denitrifiseringen av nitratet som også for ammo-nif iseringen. to the aeration container 1. In this way favorable conditions are obtained for the denitrification of the nitrate as well as for the ammonification.
Fra avsetningsbekkenet 3 tas ut oksygenfritt avvann som inneholder den ikke avsettbare del av svevestoffer såvel som ammonium over avløpsrennen 4 og ledes bort over ledningen 5 til luftningsbeholderen 6 i det annet trinn og derpå over ledningen 8 til det etterkoblete avsetningsbekken 7. I luftningsbeholderen 6 avstemmes igjen på i og for seg kjente måte luftningstiden med luft over ledningene 11 og 10 innfort oksygen-mengde og slamkonsentrasjon slik at det fra avsetningsbekkenet 7 over et overlop 15 og en ledning 16 bortflytende, nå klarete vann ennå inneholder minst 2 mg/l, fortrinnsvis 4 mg/l fritt oksygen. BOB^-slambelastningen basert på den totale slammengde i luftningsbeholderen 6 og i avsetningsbekkenet 7 er 0,1 kg BOB^ / kg slamtorrstoff. Omtrent 2/3 av den totale slammengde befinner seg stadig i luftningsbeholderen 6, 1/3 i avsetningsbekkenet 7. Den over en ledning 14 tilbakeforte slammengde utgjor 1/4 av totalvolumet i avsetningsbekkenet 7 pr. time. Ved dette skaffes gunstige betingelser for nitrifiseringen av ammoniumet i dette annet trinn. From the settling basin 3, oxygen-free waste water containing the non-separable part of suspended matter as well as ammonium is taken out via the drainage channel 4 and led away via line 5 to the aeration tank 6 in the second stage and then via line 8 to the downstream settling stream 7. In the aeration tank 6, it is adjusted again in a manner known per se, the aeration time with air over the lines 11 and 10 increases the oxygen quantity and sludge concentration so that the now clarified water flowing away from the sedimentation basin 7 over an overflow 15 and a line 16 still contains at least 2 mg/l, preferably 4 mg/l free oxygen. The BOB^ sludge load based on the total amount of sludge in the aeration tank 6 and in the settling basin 7 is 0.1 kg BOB^ / kg sludge dry matter. Approximately 2/3 of the total amount of sludge is constantly in the aeration container 6, 1/3 in the settling basin 7. The amount of sludge returned over a line 14 constitutes 1/4 of the total volume in the settling basin 7 per hour. This provides favorable conditions for the nitrification of the ammonium in this second step.
I dette trinn kan videre, for ytterligere eliminering av fosfater fra avvannet som skal renses uten å forstyrre de ovrige prosesser i dette trinn og særlig uten å forstyrre nitrifiseringen, i og for seg kjente fellingskjemikalier som aluminium-og jernsalter tilsettes over en ledning 20, og da fordelaktig for vannets innlop i avsetningsbekkenet 7 henholdsvis i luftningsbeholderen 6. In this step, for the further elimination of phosphates from the waste water to be purified without disturbing the other processes in this step and especially without disturbing the nitrification, per se known precipitation chemicals such as aluminum and iron salts can be added via a line 20, and then beneficial for the water's inflow into the settling basin 7 or into the aeration container 6.
Det har videre vist seg at det i bestemte tilfeller er fordelaktig når for forbedring av sedimenteringsegenskapene i det annet trinn også i og for seg kjente organiske og/eller uorga-niske flokkuleringsmidler, f.eks. bentonitt, cellulosefibre eller anioniske, kationiske eller ikke-ioniske flokkulerings-hjelpemidler tilsettes. Slike hjelpemidler forstyrrer på ingen måte den onskete nitrifiseringsprosess. It has also been shown that, in certain cases, it is advantageous when for the improvement of the sedimentation properties in the second stage, organic and/or inorganic flocculating agents known in and of themselves, e.g. bentonite, cellulose fibers or anionic, cationic or non-ionic flocculation aids are added. Such aids in no way interfere with the desired nitrification process.
For denitrifiseringen av det i det annet fremgangsmåtetrinn nitrifiserte ammonium og dermed for eliminering av nltratnitro-gen fra avvannet som skal renses tas bare en del, fortrinnsvis minst 50%, av det til avsetningsbekkenet 7 i 24 timer tilledete nitrifiserte avvann ut fra dette avsetningsbekken 7 og tilbake-sirkuleres til anleggets forste trinn, hvor de gunstige betingelser for denitrifiseringen av nitrifiserte nitrogenforbindelser hersker. Med fordel reguleres da anlegget slik at i det forste trinn for denitrifiseringen tilfores omtrent like meget vann fra avsetningsbekkenet 7 som dette mottar ikke renset avvann fra ledningen 12 i 24 timer. For the denitrification of the nitrified ammonium in the second method step and thus for the elimination of nitrate nitrogen from the wastewater to be purified, only a portion, preferably at least 50%, of the nitrified wastewater supplied to the sedimentation basin 7 for 24 hours is taken out of this deposition basin 7 and is re-circulated to the plant's first stage, where the favorable conditions for the denitrification of nitrified nitrogen compounds prevail. Advantageously, the plant is then regulated so that in the first step for the denitrification, approximately the same amount of water is supplied from the sedimentation basin 7 as it receives untreated waste water from the line 12 for 24 hours.
Det har vist seg fordelaktig å ta ut det vann som tilfores det forste trinn fra avsetningsbekkenet 7 i det annet trinn i en dypde på omtrent 0,2 til 2 m, fortrinnsvis 0,8 m, under vannspeilet. Uttagningen er på tegningen anskueliggjort med en ledning 17, som forer tilbake det uttatte vann til ledningen 2, hvor en intim blanding med det i det forste trinn foreliggende vann skjer. Ifolge en ikke gjengitt variant vil det også være mulig å innfore det vann som tas ut fra avsetningsbekkenet 7 for resirkulasjon i stedet for i ledningen 2 også i luftningsbeholderen 1 eller avsetningsbekkenet 3 i det forste trinn. It has proven advantageous to withdraw the water supplied to the first stage from the settling basin 7 in the second stage at a depth of approximately 0.2 to 2 m, preferably 0.8 m, below the water table. The withdrawal is visualized in the drawing with a line 17, which returns the withdrawn water to the line 2, where an intimate mixing with the water present in the first stage takes place. According to a variant not reproduced, it will also be possible to introduce the water taken from the settling basin 7 for recirculation instead of in the line 2 also into the aeration container 1 or the settling basin 3 in the first stage.
Ved denitrifiseringen i det forste trinn er slammet som folge av de i slamflokkene delvis inneholdte mikrogassblærer vanske-ligere å konsentrere. Det kan derfor være fordelaktig å avgas-se det fra dette trinn avtrukne overskuddsslam for dets innfo-ring til sedimentering i en fortykningsanordning av vanlig art. Dette kan skje ved at slammet for innforingen i fortykningsan-ordningen mekanisk rores om i 1 til 7 timer, fortrinnsvis 3 timer uten lufttilforsel i en beholder, hvorved den storste del av gassblærene fjernes. During the denitrification in the first stage, the sludge is more difficult to concentrate as a result of the microgas bubbles partially contained in the sludge flocs. It may therefore be advantageous to degas the excess sludge withdrawn from this step for its introduction to sedimentation in a conventional thickening device. This can happen by mechanically stirring the sludge for introduction into the thickening device for 1 to 7 hours, preferably 3 hours without air supply in a container, whereby the largest part of the gas bubbles is removed.
En ytterligere mulighet, å konsentrere overskuddsslammet uten at mikroblærene virker forstyrrende ved dette, kan bestå i at dette i stedet for å sedimenteres oppkonsentreres i en i og for seg kjent anordning ved flottasjon. A further possibility, to concentrate the surplus sludge without the microbubbles having a disruptive effect on this, can consist in this instead of being sedimented being concentrated in a device known per se by flotation.
Claims (10)
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DE2426672C3 (en) * | 1974-06-01 | 1980-04-24 | Bayer Ag, 5090 Leverkusen | Process for the recoagulation of activated sludge flakes and a suitable recoagulator |
JPS5161178A (en) * | 1974-11-22 | 1976-05-27 | Maruzen Oil Co Ltd | |
US3994802A (en) * | 1975-04-16 | 1976-11-30 | Air Products And Chemicals, Inc. | Removal of BOD and nitrogenous pollutants from wastewaters |
SE405351C (en) * | 1975-04-25 | 1987-06-10 | Svenska Sockerfabriks Ab | PROCEDURE FOR BIOLOGICAL CLEANING OF CARBOHYDRATE AND / OR PROTEINRIC WASTE WATER |
JPS51127570A (en) * | 1975-04-28 | 1976-11-06 | Sumitomo Chem Co Ltd | Method for treating waste water containing nitrate nitrogen and/or nit rite nitrogen |
CH621751A5 (en) * | 1976-09-24 | 1981-02-27 | Attisholz Cellulose | Process for the biochemical purification of waste water containing organic constituents which favour the undesirable development of filamentous bacteria and/or the formation of bulking sludge |
JPS53125359A (en) * | 1977-04-06 | 1978-11-01 | Niigata Eng Co Ltd | Method of removing nitrogen in waste water by non woven web plate |
DE2803759C3 (en) * | 1978-01-28 | 1983-01-13 | Böhnke, Botho, Prof. Dr.-Ing. | Two-stage system for the treatment of wastewater according to the activated sludge process |
DE2909168C2 (en) * | 1979-03-08 | 1983-10-27 | August Dr.-Ing. Schreiber | Process and device for the aerobic and anaerobic treatment of waste water |
DE2918950A1 (en) * | 1979-05-10 | 1980-11-20 | Linde Ag | METHOD AND DEVICE FOR NITRIFICATION AND DENITRIFICATION OF SEWAGE |
DE3002604A1 (en) * | 1980-01-25 | 1981-07-30 | Basf Ag, 6700 Ludwigshafen | METHOD AND DEVICE FOR BIOLOGICAL WASTE WATER TREATMENT |
DE3206527A1 (en) * | 1982-02-24 | 1983-09-01 | Linde Ag, 6200 Wiesbaden | METHOD AND DEVICE FOR BIOLOGICAL NITRIFICATION OF WASTEWATER |
AT396684B (en) * | 1991-08-06 | 1993-11-25 | Norbert Dipl Ing Dr Te Matsche | Activated sludge process for the purification of waste water |
US5447633A (en) * | 1991-08-06 | 1995-09-05 | Austrian Energy & Environment Sgp/Waagner Biro Gmbh | Activated sludge process for sewage purification |
AT397382B (en) * | 1992-01-14 | 1994-03-25 | Ingerle Kurt Dipl Ing Dr Techn | METHOD FOR DENITRIFYING WASTEWATER |
WO2000005177A1 (en) * | 1998-07-24 | 2000-02-03 | Dhv Water B.V. | Process for the treatment of waste water containing specific components, e.g. ammonia |
GB0006552D0 (en) | 2000-03-17 | 2000-05-10 | For Research In Earth And Spac | System for removing phosphorus from waste water |
GB0230309D0 (en) * | 2002-12-31 | 2003-02-05 | Wrc Plc | Procedure for enhancing removal of ammonia in the activated sludge process for treatment of wastewaters |
KR101162474B1 (en) * | 2004-02-02 | 2012-07-03 | 쿠리타 고교 가부시키가이샤 | Process for biological treatment of organic waste water and apparatus therefor |
CN115465953B (en) * | 2022-10-19 | 2023-09-22 | 大连安能杰科技有限公司 | AOD biochemical reaction system for treating sewage and sewage treatment method thereof |
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GB1406839A (en) | 1975-09-17 |
DK141868C (en) | 1980-11-24 |
IE36689B1 (en) | 1977-02-02 |
IL40289A (en) | 1975-02-10 |
IT962707B (en) | 1973-12-31 |
CA986627A (en) | 1976-03-30 |
FR2160799A1 (en) | 1973-07-06 |
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DK141868B (en) | 1980-07-07 |
BE787184A (en) | 1972-12-01 |
JPS4859659A (en) | 1973-08-21 |
FI55824B (en) | 1979-06-29 |
NO134045C (en) | 1976-08-11 |
NL7208783A (en) | 1973-05-25 |
AT318503B (en) | 1974-10-25 |
AU4631272A (en) | 1974-03-14 |
DE2233801B2 (en) | 1978-05-11 |
SE374340B (en) | 1975-03-03 |
IL40289A0 (en) | 1972-11-28 |
DE2233801A1 (en) | 1973-05-30 |
JPS5643797B2 (en) | 1981-10-15 |
IE36689L (en) | 1973-05-23 |
FI55824C (en) | 1979-10-10 |
CH547235A (en) | 1974-03-29 |
FR2160799B1 (en) | 1978-03-03 |
ZA726121B (en) | 1973-05-30 |
BR7205090D0 (en) | 1973-09-20 |
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