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WO1998030504A1 - Evacuation aeree de substances polluantes azotees presentes dans des eaux usees biologiquement degradables - Google Patents

Evacuation aeree de substances polluantes azotees presentes dans des eaux usees biologiquement degradables Download PDF

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Publication number
WO1998030504A1
WO1998030504A1 PCT/AU1998/000011 AU9800011W WO9830504A1 WO 1998030504 A1 WO1998030504 A1 WO 1998030504A1 AU 9800011 W AU9800011 W AU 9800011W WO 9830504 A1 WO9830504 A1 WO 9830504A1
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WIPO (PCT)
Prior art keywords
reactor
volume
admixture
wastewater
air
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Ceased
Application number
PCT/AU1998/000011
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English (en)
Inventor
Mervyn Charles Goronszy
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BISASCO PTY Ltd
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BISASCO PTY Ltd
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Publication date
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Priority to SI9820017A priority Critical patent/SI20157A/sl
Priority to AU54686/98A priority patent/AU5468698A/en
Publication of WO1998030504A1 publication Critical patent/WO1998030504A1/fr
Anticipated expiration legal-status Critical
Ceased legal-status Critical Current

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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
    • C02F3/006—Regulation methods for biological 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
    • C02F3/302—Nitrification and denitrification 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
    • C02F3/32—Biological treatment of water, waste water, or sewage characterised by the animals or plants used, e.g. algae
    • C02F3/327—Biological treatment of water, waste water, or sewage characterised by the animals or plants used, e.g. algae characterised by animals and plants
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/04—Oxidation reduction potential [ORP]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/10—Solids, e.g. total solids [TS], total suspended solids [TSS] or volatile solids [VS]
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/22—O2
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/42—Liquid level
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2209/00—Controlling or monitoring parameters in water treatment
    • C02F2209/44—Time
    • 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

Definitions

  • the present invention relates to a method of removal nitrogenous and other nutrient pollutants and carbonaceous oxygen demand from industrial and domestic wastewaters using cyclically aerated activated sludge processing.
  • the present invention provides a method for the acclimated combined growth of heterotrophic and autotrophic micro-organisms for the removal of nitrogen, organics and other nutrient pollutants in a wastewater using an admixture reactor, comprising the steps of: providing an initial admixture of influent wastewater with a flow of acclimated culture, from a second sequentially aerated reactor volume, at least during an unmixed unaerated time period followed by an aerated - mixed time period, causing the oxidation reduction potential of the mixture to progressively decrease in the admixture reactor to less than about -100 mV to about -200 mV (when compared to a hydrogen reference electrode).
  • the time cycles, and equipment interaction of each reactor are automatically controlled.
  • sensors for the measurement of oxidation - reduction potential, dissolved oxygen concentration, mixed liquor suspended solids concentration are in contact with a velocity stream of said mixture at least during an aeration period.
  • the mixture suspended solids concentration in the second reactor volume at bottom water level is about 5000 to 6000 mg/L with an operating sludge age that provides the proliferation of the autotrophic micro-organisms for a designated range of operating temperature and effluent nitrogen concentrations.
  • a stoichiometric mass of process oxygen in a cycle is transferred during preselected sequences of time and set point dissolved oxygen concentrations.
  • the acclimated culture contains general higher life forms, such as Vorticella. Ciliates. Protozoa. Rotifer. Nematodes and the like.
  • the step of controlling the decrease in the oxidation reduction potential to below about -200 mV (compared to reference hydrogen electrode) in the admixture volume is done by means of entrainment of selectively placed oxygen containing gas bubbles.
  • the near surface liquid removal rate that takes place in an air off sequence is process compatible and does not cause the entrainment of solids from within the settled solids layer.
  • a plurality of reactors are used, whereby the net flow in and out of the plurality of reactors is continuous whereby flow into and out of each reactor is interrupted for at least a part of the time.
  • the varying volume is produced by a moving box weir within the reactor connected by a plurality of downcomers to a central rotating drum shaft for moving the weir to a set bottom water level position and then returning it to an out of liquid rest position.
  • the present invention provides apparatus for the removal of nitrogen, organics and other pollutants in a wastewater using an admixture reactor by the acclimated combined growth of heterotrophic and autotrophic microorganisms, comprising:: means for continuously providing an initial admixture of influent wastewater with a flow of acclimated culture, from a second sequentially aerated reactor volume.
  • the invention incorporates the use of cyclically aerated activated sludge processing for the removal of nitrogenous pollutants and carbonaceous oxygen demand from industrial and domestic wastewaters.
  • the invention relates to the design and operation of a wastewater - activated sludge admixing reactor which is configured to efficiently function for mixing and particle nucleation using high liquid velocities through orifice jetting at a stationary wall position and much lower coagulating - flocculating liquid velocities at surface air interfaces which, combined. promote to floe nucleation and growth, in a multi-cell arrangement.
  • the admixing volume is connected, by pipe or other hydraulic means, to a second reactor volume which is subject to cycled aeration sequences.
  • This form of the invention combines an activated sludge reactor configuration operated for repetitive sequenced positive to negative oxidation reduction potential cycling and treated effluent removal using a lowering box weir decanter connected to a rotating drum shaft by a plurality of downcomers for the removal of BOD and nitrogen through simultaneous aerated nitrification - denitrification.
  • Admixing of biodegradable wastewater with an activated sludge microbial catalyst under defined conditions of relative flow proportions and mixing energy determine the net floe size (mean diameter) of the activated sludge and its liquid phase oxidation reduction potential.
  • True anaerobic conditions, with sulfide generation. require an oxidation - reduction potential (reference hydrogen electrode) of about -400 mV.
  • highly aerated mixtures of wastewater and activated sludge exhibit an oxidation reduction potential of about 300 mV. It is known that numerous biological reactions can be facilitated through exposure to reaction conditions delineated by oxidation reduction potential.
  • the terms oxic. anoxic and anaerobic which have conventional (historical) definition, became meaningless as we have found it possible to generate biological reactions under aerated conditions (oxic by former definition) which have been known to require anoxic conditions (by former definition).
  • the admixture volume can also be designed to operate as a surface grease and oil collector which then requires its own removal management considerations.
  • Figure 1 shows a graph of SQR/AOR variation with basin dissolved oxygen concentration achieved with an embodiment of the invention
  • Figure 2 shows nitrification equations in accordance with an embodiment of the invention
  • FIG. 3 shows a schematic diagram of the processing system according to one embodiment of the invention
  • Figure 4 shows a schematic diagram of one module of the system of Figure 3:
  • FIGS 5-9 show various shapes of the basins which may be used in embodiments of the invention.
  • Figures 10 and 1 1 show two forms of cross sectional shape of the basins which may be used in embodiments of the invention; and Figure 12 shows a schematic cross sectional view of a typical admixture structure according to one embodiment of the invention.
  • the admixture volume can be of any geometry.
  • For effective nitrogen removal from typically medium strength domestic wastewaters requires an admixture volume of around 40 minutes mean retention time at average dry weather flow conditions.
  • Sparge pipes, or other gas injection means are strategically located in upward flowing segments of the admixture volume to effect, when required, short term (less than 21 minute) preprogrammed operation for oxygen reduction potential (ORP) modification.
  • ORP oxygen reduction potential
  • Upflow velocities in the admixture volume are designed to be non-settling for most expected particle sizes.
  • Special raw wastewater circumstances such as high dissolved oxygen (in excess of 2 mg/L).
  • low readily available soluble substrate less than 30 mg/L).
  • low BOD/TKN ratio less than 3.0/1 require a special design of admixture reactor which includes an ability to provide hydrolysis of influent readily degradable particulate substrate, among other related factors. Elements of the design and mode of operation are very important to the functions of biological nitrification and denitrification as designed and intended for a works; and also to the net use of readily degradable soluble substrate and to the hydrolysis of readily degradable particulate substrate to soluble readily degradable substrate.
  • 1 mg of influent degradable VSS generates about 1.4 mg of equivalent readily degradable soluble COD.
  • the preferred admixture volume embodiment is essentially designed to operate as a plug-flow unit through a multi-cellular arrangement that will insure a high degree of dispersion. It should be configured and fitted to provide selectable reaction environments within a cell or in successive cells.
  • the admixture volume can function as totally aerobic, initially anoxic and then anaerobic then anoxic to anaerobic, initially aerobic then anoxic to anaerobic and then anoxic to aerobic etc. etc.
  • the specific environment - reaction time can be manipulated simply through operating selected valves: open, closed or partially open and intermittently used.
  • the preferred admixture embodiment is designed to operate within a range of substrate to microorganism ratios without flow adjustment.
  • the primary design and function of the admixture volume is to maximize enzymatic transfer of the readily degradable (soluble) fraction of the influent organics which is then followed by depletion of the liquid phase oxidation reduction potential.
  • receptive microorganisms are provided with a saturated substrate environment to enhance initial rates of substrate removal and maximize the mass conversion to the collectively called intracellular - storage compounds. In so doing advantage is taken of substrate affinity which is influenced by both micro-organism growth rate and the ratio(s) of substrates available.
  • heterotrophic bacteria to increase their uptake affinity for limiting nutrients is well documented, particularly for sugars and for phosphate with depression of catabolic enzymes as the most commonly described regulation mechanism.
  • Alternative pathways can be forced when an environmental condition such as oxygen tension can be used to limit metabolic access to the substrate carbon source.
  • the oscillating feed starve mechanism of operation of the two reactors in combination enhances general storage product formation and oxidation reduction potential of the reaction environments..
  • the principle behind the design is to provide for the capture of a soluble carbon source under maximum controlled conditions and to direct that carbon source so that it is available in a controlled environment that permits the removal of ammonia and provides an electron balance velocity whereby the ammonia oxidation product is essentially removed as a nitrogen containing gas.
  • a large overall aerobic reactor fraction enhances the physical storage transfer and subsequent use therein.
  • Feeding substrate in an oxygen limited environment also results in maximum polymer formation.
  • Feeding substrate in an oxygen limited environment also results in maximum polymer formation.
  • the metabolic pathway for organic carbon use is relatively well known. Firstly under aerated conditions, heterotrophic removal utilizes organic carbon as its carbon and energy sources for oxidation and phosphorus polymerization. In this case the organic matter degradation follows the glycolysis/pyruvic acid/Krebs cycle metabolic pathways. This scheme is highly efficient in terms of energy production, yielding 38 ATP (Adenosine Triposphate) molecules per mole of glucose oxidized. This is the principle reason that this mechanism is the preferred scheme over other possible pathways, in the presence of free dissolved oxygen.
  • Glycogen is a glucose polymer which provides cells with a reserve of carbohydrate. Its degradation is accomplished through the glycolysis pathway. End products will depend upon the prevailing environmental conditions. The glycolysis pathway is also used for its synthesis, in the reverse way.
  • Carbon dioxide and intermediary products of the Krebs cycle are used as substrates for the synthesis of glycogen, when there is a surplus of exogenous organic material and ATP is not needed by the cell.
  • Nitrification is traditionally concluded to be a two stage reaction (simplified).
  • the first stage pathway is believed to occur in three steps, from an oxidation state of -3 to +3. It is believed that energy derives from the oxidation of hydroxylamine (NH 2 0H) and that ATP is produced by oxidative phosphorylation when the electrons pass through the electron transport chain.
  • nitrifiers are strictly aerobic when growing on their respective substrate: anoxic or anaerobic conditions are not lethal to them. Under these conditions it has been shown that Nitrobacter can reduce nitrate and that Nitrosomonas europa can reduce nitrite in the presence of hydroxylamine. The overall equation for nitrifier synthesis and nitrification is written as
  • Nitrifier cell yield is 0.17 g cells/g NH 4 .N removed.
  • Alkalinity reduction is 8.63 g HC0 3 /g NH 4 _N removed or 7.14 CaC0 3 /gNH 4 N removed.
  • the enzyme assimilatory nitrate reduction catalyzes the transformation of nitrate to ammonia by following the inverse mctabloic rate of nitrification, the resulting ammonia being used for synthesis. This mechanism takes place in the presence of dissolved oxygen. Denitrification is written as
  • Reduction of nitrate to nitrite occurs by enzyme dissimilatory nitrate reduction, utilizing electrons from cytochrome b of the electron transport chain.
  • Both PHB and glycogen can provide the organic carbon for denitrifiction. This factor is maximized in the use of the preferred admixture volume embodiment.
  • ammonia oxidation can be controlled as to the formation of nitrite and nitrate nitrogen.
  • Operation under reaction conditions with an excess of ammonia and a limit on the mass supply of process oxygen promotes a removal of ammonia nitrogen with an increase in oxidized nitrogen as the limitation on oxygen supply is removed.
  • DO is also limiting being generally less than 0.1 mg/L.
  • Nitrosomonas species that rapidly assimilates nitrite or nitrate nitrogen under aerated positive dissolved oxygen reaction conditions.
  • the multi-cell admixture volume is sized to maximize the rate of depletion liquid phase of oxidation reduction potential, i.e. to make sure participating microorganisms approach an initial saturated storage state. Recognizing that the introduction sludge is at a reduced metabolic activity as measured by an SOUR of around 7 - 10 mg0 2 /gVSS/hr. In the initial admixture volume (measured under artificial dissolved oxygen concentration enhancement) this rate escalates by a factor of 3+ representing the advanced level of enzymatic transfer of the available substrate. Measurements taken in full-scale reactors have always shown the level of concentration dynamics as described above. Using biomass that exhibits endogenous reactivity (OUR) only it is not possible to maintain the same level of aerated nitrogen removal.
  • OUR endogenous reactivity
  • the admix reactor design maximizes soluble substrate uptake caused by elevated substrate to biomass loading, reduces (markedly) the liquid phase oxidation reduction potential, assists with the hydrolysis of particulate BOD to soluble compounds that are immediately enzymatically removed, causes release of polyphosphate, thus generating a highly reactive stored carbon source.
  • Operation at a dissolved oxygen limitation of 0, 1 , 2.5 mg/L. results in a beneficial AOR/SOR ratio relative to energy use (air flow rate) and ⁇ : dissolved oxygen differential as shown in Figure 1 for Alpha of 0.65, Beta.98. 100 metres elevation).
  • Stopping the reaction at the nitrite stage represents a used 1.5 moles of oxygen in place of two moles used for the conventional nitrate formation. This may convert to a 25 percent oxygen saving alone. On the other hand, only 0.5 moles of oxygen may be required for the nitrate formation reaction.
  • Ammonia nitrogen is removed by assimilation into micro-organisms.
  • the nitrogen contained therein can be. through digestion processes, made available for either nitrite or nitrate formation.
  • aeration input is designed to operate under a stepped - time dissolved oxygen profile.
  • the first step is at or near zero dissolved oxygen; the second step is less than 1.0 mg/L; the third step is greater than 1.0 mg/L but less than 2.5 mg/L.
  • the upper maximum operating dissolved oxygen is itself functional on the end of aeration sequence dissolved oxygen concentration.
  • the duration of each step depends upon the operating cycle. Discounting the non-aerated fill sequence and by way of example a four hour cycle, the first step is likelv to be for 60-80 minutes, the second step 20-40 minutes and the third step 20-40 minutes. The remainder of the time is allocated to solids liquid separation and to effluent withdrawal. Other time cycles can be used with shortened stepped times. This mode of operation is an effective shunt to the growth of Nitrobacter and hence the formation of nitrite with the caveat that process oxygen is made available at a rate that meets oxygen demand.
  • the admixture preferred embodiment is designed to function principally between two modes, positive to negative redox potential. (The status of the soluble compounds in the wastewater during commissioning will determine the exact method of operation). For phosphorus removal we need a generation of starved PHB or PHV. These stored carbon compounds are effective carbon sources for denitritification and denitrification. Alternatively the same nitrogen removal processes can be obtained through the glycogen pathway.
  • the preferred reactor embodiment has as a minimum provision for hydrolysis of readily degradable influent particulate substrate.
  • wastewater to be treated in this process may have passed through any number of combinations of pre-treatment unit operations which may include screening, grit removal, oil and grease removal, primary settling, pH correction, alkalinity addition, nutrient addition.
  • the treatment system may have four reactor modules 1 into which influent wastewater is directed according to a set and predetermined flow sequence.
  • Each module as shown in Figure 4. contains a constructed reaction volume for cyclical aeration and non-aeration 2; a constructed volume for the addition of raw influent with a flow of biomass from the constructed reaction volume at least during an aeration sequence 3, whereby mixing takes place naturally and with out mechanical equipment, a means 4 for stopping the flow of influent wastewater (motorised valve or weir gate), a pump means 5 for directing reaction volume contents to the admixture volume .
  • a pump means 6 for the removal of waste biomass from either the reactor volume or the admixture volume 2, an oxygen transfer means 7 for the generation of air bubbles during the pumping of air thereto 8.
  • a moving weir liquid conveyance mechanism 9 driven by motor means 10 to cause layers of near surface liquid to be collected in a horizontally configured box via a plurality of pipes 1 1 connecting the horizontal box to a central rotating drum shaft which transports the collected liquid out of the reactor volume by gravity.
  • the horizontally configured box is positioned such that the leading edge, which is fitted with an adjustable weir, accepts the flowing supernatant liquid from a near surface position with the use of an attached self moving floating screen guard which positively excludes surface solids.
  • each module will operate to transport up to 2.5 metres of liquid depth of near surface waters and to contain up to a bout 3.5 metres of liquid depth after the near surface liquid removal operation.
  • Each module houses sensing instrumentation 13, 14, 15 and 16 for the automatic monitoring of dissolved oxygen concentration 13, oxidation reduction potential 14, mixed liquor suspended solids concentration 15, and liquid depth 16. The sensors 13, 14.
  • the setting of the duration for oxygenation in each aeration cycle is important to the processing technique which regulates the various enzyme, catalyse and intracellular storage mechanisms.
  • the initial enzyme transfer and subsequent intracellular storage mechanisms which are caused to take place at greater than 100 mV (hydrogen scale reference), less than 0 mV and at a pH that is not less than 6.0 units it is possible to select a biological culture and biological reaction circumstance which does not determinate at the nitrate form.
  • By adhering to these principles of operating it becomes possible to cause the removal of ammonia nitrogen, presumably to terminal completion to nitrogen or nitrogen containing gases without the major formation and accumulation of nitrate nitrogen.
  • each air-on time sequence is a process variable from cycle to cycle as is the aeration intensity within a cycle.
  • a portion of the sludge is pumped for admixture with the incoming wastewater at least during an aeration sequence.
  • a portion of the sludge in the second reactor is removed at least during an air-off sequence. While multiple basins present the optimum embodiment, for the process of the invention it may be practised in a single treating basin with the reactor volumes as described. It will be clear to those experienced in the art that an individual module can have a number of alternative cross sections, and arrangements to make best use of common wall construction.
  • the enclosing structure can be of either upright construction or sloping wall construction. Regular, rectangular, square, circular and octagonal quadrant. These various shapes and configurations are illustrated in Figures 5 to 9.
  • Figure 12 there is shown a cross sectional view of the admixture reactor according to one embodiment.
  • the inflow enters through port 20 and flows as indicated through a number of baffles 21 to the second zone.
  • the baffles and mixture flows are arranged to provide the desired operating conditions. Sludge is fed back from the second zone through pipe 22.

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  • Water Supply & Treatment (AREA)
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Abstract

Procédé et dispositif de traitement cyclique de boues activées utilisant des installations à multiréacteurs (généralement 2, 3, 4 ou des multiples de 2, dont 6, 8, 12, 16, etc.) sans clarificateurs secondaires séparés, permettant une adaptation à un profil hydraulique continu. Chaque réacteur reçoit un volume de matière mélangée constituant une zone de mélange d'origine non aérée suivie de pentes d'écoulement répétitives de façon à nucléer et favoriser la formation de flocs de grande taille de boues activées, suivies d'une seconde zone de réaction aérée par intermittence et connectée hydrauliquement au moyen d'un système à chicanes partielles. La seconde zone de réaction dans chaque réacteur est actionnée collectivement, mais hors phase, au moyen de séquences successives d'entrée et de sortie d'air. La séquence de sortie d'air permet une séparation solides-liquide et un tarissement du potentiel d'oxydoréduction de la biomasse après une séquence d'entrée d'air, avec un retrait ultérieur d'une fraction du contenu liquide se trouvant au niveau supérieur dans le réacteur au moyen d'un décanteur déversoir à boîte mobile à vitesse variable. Les boues contenant des micro-organismes hétérotrophes et autotrophes sont envoyées de la seconde zone vers le volume d'origine pour être ajoutées aux eaux usées biodégradables présentant un rapport de BOD:TKN supérieur à 3:1. La durée de chaque séquence d'entrée d'air dépend de l'entrée de la charge de la masse à demande relative en oxygène. L'invention prévoit un écoulement entrant au cours d'une séquence prolongée de sortie d'air après le retrait de la fraction du liquide surnageant. La séquence d'entrée d'air s'effectue normalement avec le remplissage d'un influent dans le réacteur. Les séquences d'entrée d'air dans le volume du second réacteur sert à mélanger le potentiel d'oxydoréduction de la culture de micro-organismes séparés et déposés et à l'élever d'une valeur négative à une valeur positive mélangée. Les séquences de sortie d'air dans le volume du second réacteur fournissent des phases liquide-solides séparées avec un tarissement dynamique vers un potentiel d'oxydoréduction négatif (environ -150mV comparé à une électrode de référence à hydrogène).
PCT/AU1998/000011 1997-01-09 1998-01-09 Evacuation aeree de substances polluantes azotees presentes dans des eaux usees biologiquement degradables Ceased WO1998030504A1 (fr)

Priority Applications (2)

Application Number Priority Date Filing Date Title
SI9820017A SI20157A (sl) 1997-01-09 1998-01-09 Prezračevano odstranjevanje dušikovih onesnaževalcev iz biološko razgradljivih odpadnih voda
AU54686/98A AU5468698A (en) 1997-01-09 1998-01-09 Aerated removal of nitrogen pollutants from biologically degradable wastewaters

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AUPO4538A AUPO453897A0 (en) 1997-01-09 1997-01-09 Improvements in wastewater treatment processing
AUPO4538 1997-01-09

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Cited By (11)

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GB2369115A (en) * 2000-11-17 2002-05-22 Kwangju Inst Sci & Tech Simultaneous removal process of nitrogen and phosphorus in wastewater
CN102079611A (zh) * 2010-12-17 2011-06-01 重庆科瑞制药有限责任公司 一种污水处理自控方法
CN102249483A (zh) * 2011-05-16 2011-11-23 南京大学 利用cass工艺和塔式蚯蚓生态滤池处理工业废水的方法
CN102653436A (zh) * 2012-06-01 2012-09-05 中冶华天南京工程技术有限公司 污水回用处理系统及工艺
WO2014043547A1 (fr) * 2012-09-13 2014-03-20 D.C. Water & Sewer & Authority Procédé et appareil pour l'élimination d'azote dans un traitement d'eaux usées
US9340439B2 (en) 2012-09-13 2016-05-17 D.C. Water & Sewer Authority Method and apparatus for nitrogen removal in wastewater treatment
WO2016202628A1 (fr) 2015-06-16 2016-12-22 Inwatech Enviromental Kft. Procédé de traitement aérobie d'un flux d'eaux usées biodégradables
CN112093890A (zh) * 2020-07-31 2020-12-18 国投信开水环境投资有限公司 一种短程硝化处理污水的方法
CN113562837A (zh) * 2021-08-11 2021-10-29 江苏亿尚景水务有限公司 一种固定化微生物载体填料及其制备方法
CN114477444A (zh) * 2022-04-19 2022-05-13 北京涞澈科技发展有限公司 一种自养异养协同反硝化一体化装置及污水处理方法
CN115594289A (zh) * 2022-09-30 2023-01-13 南开大学（Cn） 一种采用低浓度碳源培养驯化电活性降解微生物膜的方法、一种石化废水的处理方法

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CN102079611A (zh) * 2010-12-17 2011-06-01 重庆科瑞制药有限责任公司 一种污水处理自控方法
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US9340439B2 (en) 2012-09-13 2016-05-17 D.C. Water & Sewer Authority Method and apparatus for nitrogen removal in wastewater treatment
JP2015531683A (ja) * 2012-09-13 2015-11-05 ディー．シー． ウォーター アンド スーアー オーソリティー 廃水処理における脱窒の方法及び装置
CN105189368A (zh) * 2012-09-13 2015-12-23 华盛顿特区供水和污水管理局 用于在废水处理中脱除氮的方法和装置
WO2014043547A1 (fr) * 2012-09-13 2014-03-20 D.C. Water & Sewer & Authority Procédé et appareil pour l'élimination d'azote dans un traitement d'eaux usées
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