WO2015052279A1 - Méthode et système d'élimination de l'azote d'eaux usées - Google Patents

Méthode et système d'élimination de l'azote d'eaux usées Download PDF

Info

Publication number
WO2015052279A1
WO2015052279A1 PCT/EP2014/071636 EP2014071636W WO2015052279A1 WO 2015052279 A1 WO2015052279 A1 WO 2015052279A1 EP 2014071636 W EP2014071636 W EP 2014071636W WO 2015052279 A1 WO2015052279 A1 WO 2015052279A1
Authority
WO
WIPO (PCT)
Prior art keywords
biofilm reactor
ammonium
concentration
reactor
outlet
Prior art date
Application number
PCT/EP2014/071636
Other languages
English (en)
Inventor
Julián CARRERA MUYO
Eduardo ISANTA MONCLÚS
Julio PÉREZ CAÑESTRO
Original Assignee
Universitat Autonoma De Barcelona
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Universitat Autonoma De Barcelona filed Critical Universitat Autonoma De Barcelona
Publication of WO2015052279A1 publication Critical patent/WO2015052279A1/fr

Links

Classifications

    • 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
    • C02F3/303—Nitrification and denitrification treatment characterised by the nitrification
    • 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
    • C02F3/307—Nitrification and denitrification treatment characterised by direct conversion of nitrite to molecular nitrogen, e.g. by using the Anammox process
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F11/00—Treatment of sludge; Devices therefor
    • C02F11/02—Biological treatment
    • C02F11/04—Anaerobic treatment; Production of methane by such processes
    • 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
    • C02F2209/003—Downstream control, i.e. outlet monitoring, e.g. to check the treating agents, such as halogens or ozone, leaving the process
    • 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
    • C02F2209/14—NH3-N
    • 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
    • C02F2209/15—N03-N
    • 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
    • C02F2209/40—Liquid flow rate

Definitions

  • the present invention generally relates, in a first aspect, to a method for wastewater nitrogen removal, which comprises performing a partial nitritation of wastewater in a biofilm reactor by means of an ammonium concentration closed loop control, and more particularly to a method comprising varying the ammonium concentration setpoint for the closed loop control based on nitrogen concentration.
  • a second aspect of the invention relates to a system adapted to implement the method of the first aspect.
  • the main challenge for the success of the treatment is the difficulty of maintaining stable the nitritation process, since nitrite- oxidizing bacteria (NOB) may develop in such a granular sludge, producing nitrate, competing with anammox for nitrite and reducing the efficiency of the treatment considerably.
  • NOB nitrite- oxidizing bacteria
  • ES2334321 B1 and Bartroli et al., 2010 disclose a partial nitritation method of wastewater in a biofilm reactor containing ammonia-oxidizing bacteria, comprising performing a closed loop control for regulating the ammonium concentration within the biofilm reactor based on the ammonium concentration at the outlet of the biofilm reactor.
  • the method disclosed in ES2334321 B1 is applied to wastewater with a high ammonium concentration, the goal of said method is to obtain a full nitritation, and therefore the ammonium set point is set to a fixed low value, independently of inflow characteristics, which makes the obtained effluent unsuitable for feeding, among others, an anammox reactor.
  • the method for wastewater nitrogen removal of the first aspect of the invention comprises performing a partial nitritation of wastewater in a biofilm reactor, wherein said biofilm reactor contains ammonia-oxidizing bacteria, and the method comprises performing a closed loop control for regulating the ammonium concentration within said biofilm reactor based on the ammonium concentration at the outlet of said biofilm reactor.
  • the method of the first aspect of the invention comprises calculating and varying the value of an ammonium concentration setpoint of said closed control loop based at least on the nitrogen concentration at the outlet of or inside said biofilm reactor.
  • Said nitrogen concentration generally refers to the sum of nitrite and nitrate concentrations at the outlet or inside said biofilm reactor.
  • ammonium enters the biofilm reactor through a main stream, in which case, for a preferred embodiment, the method comprises performing said regulation of ammonium concentration within the biofilm reactor by regulating the flow-rate of a side stream also entering said biofilm reactor.
  • Said ammonium concentration at the outlet of said biofilm reactor and/or said nitrogen concentration at the outlet of or inside the biofilm reactor is/are online measured (preferably both of them), whether directly at said points of the biofilm reactor (at the outlet thereof, for the ammonium concentration, and at the outlet or inside the biofilm reactor, for the nitrogen concentration), near said points, or in another point or points of the system (within or external to the biofilm reactor) which allow a calculation/estimation of the ammonium concentration at the outlet of the biofilm reactor and/or of said nitrogen concentration at the outlet of or inside the biofilm reactor from the measurements made at said another point or points of the system.
  • the method of the first aspect of the invention comprises calculating and varying the value of the ammonium concentration setpoint of the closed control loop also based on a desired ratio of ammonium and nitrite concentrations at the outlet of said biofilm reactor, hence the method can be used for feeding a further stage with an effluent having the specific ratio of ammonium and nitrite concentration required for that further stage.
  • TAN refers to the total ammonium concentration
  • SP to setpoint NO ⁇ is the sum of nitrite and nitrate
  • b to said desired ratio of ammonium and nitrite concentrations.
  • said desired ratio of ammonium and nitrite concentration is between 0.5 and 2, preferably between 1.1 and 1 .3.
  • the method of the first aspect of the invention further comprises, for a preferred embodiment, feeding an anammox reactor with the effluent of the biofilm reactor, and using said anammox reactor for performing an anammox reaction with the ammonium and nitrite contained in said biofilm reactor effluent in order to achieve a further nitrogen removal.
  • Said preferred ratio of ammonium and nitrite concentration of between 1 .1 and 1 .3 is optimal for the feeding of said annamox reactor, and thus is used therefor.
  • the problem previously described in the Background of the Invention section related to the NOB developing is circumvented, as maintaining partial nitritation without nitrate production (i.e. repressing NOB activity) is achieved by the method of the first aspect of the invention, particularly by means of the control strategy described above, thus enhancing the good efficiency of the nitrogen removal for main stream.
  • the ranges of operating conditions for the partial nitritation are: temperature inside the biofilm reactor is between 8 and 35 °C, the ammonium concentration in said main stream is between 30 and 100 g N/m 3 and the COD (Chemical Oxygen Demand) concentration is between 1 and 125 g/m 3 .
  • temperature inside the biofilm reactor is between 8 and 35 °C
  • the ammonium concentration in said main stream is between 30 and 100 g N/m 3
  • the COD (Chemical Oxygen Demand) concentration is between 1 and 125 g/m 3 .
  • said side stream carries reject water coming from an anaerobic digester, the method comprising performing said regulation of the flow-rate of said side stream from a discharging buffer tank interspersed between said anaerobic digester and the biofilm reactor.
  • the main stream comes from a main output of a very-high-load activated sludge and settler producing biomass and organic particles and feeding with the same said anaerobic digester through, the anaerobic digester generating biogas and said reject water from the received biomass and organic particles.
  • the method of the first aspect of the invention further comprises controlling the dissolved oxygen concentration inside the biofilm reactor based on the nitrogen concentration in the main stream.
  • a second aspect of the present invention concerns to a system for wastewater nitrogen removal, comprising:
  • a closed loop control configured and arranged for regulating the ammonium concentration within said biofilm reactor based on the ammonium concentration at the outlet of said biofilm reactor, said closed loop control comprising an ammonium concentration setpoint.
  • the system of the second aspect of the invention comprises processing means configured and arranged for calculating and varying the value of the ammonium concentration setpoint of said closed control loop based at least on the nitrogen concentration at the outlet of or inside the biofilm reactor.
  • the system of the second aspect of the invention comprises first and second measuring means for, respectively, measuring the ammonium concentration at the outlet of the biofilm reactor and the nitrogen concentration (particularly the sum of nitrite and nitrate concentrations) at the outlet of or inside the biofilm reactor, said first and second measuring means being arranged to provide said processing means with the measured values, the processing means being configured for performing said calculation of the value of the ammonium setpoint based on said measured values and on a desired ratio of ammonium and nitrite concentrations at the outlet of said biofilm reactor.
  • system of the second aspect of the invention further comprises:
  • a very-high-load activated sludge and settler having an input for receiving sewage, a main output connected to a main stream input of the biofilm reactor for providing the latter with ammonium, being configured for producing biomass and organic particles therefrom, and having a secondary output for delivering said biomass and organic particles;
  • an anaerobic digester having an input connected to said secondary output of the very-high-load activated sludge and settler to receive said biomass and organic particles, and being configured to generate biogas and reject water there from, through respective first and second outputs;
  • a discharging buffer tank arranged for receiving said reject water from said second output of said anaerobic digester and for feeding the biofilm reactor, through a side stream input thereof, with said reject water according to a flow-rate regulated under the control of said control means in order to perform said regulation of the ammonium concentration within the biofilm reactor;
  • the biofilm reactor (with its associated ammonium loop control) of the system of the second aspect of the invention can be connected to stages other than the ones of the above cited very-high-load activated sludge and settler, digester and anammox reactor, or in combination with some of said cited stages (generally with the anammox stage).
  • the system of the second aspect of the invention is adapted to implement the method of the first aspect.
  • Figure 1 schematically shows a conventional sewage treatment with Anammox, basic configuration (based on Kartal, Kuenen and van Loosdrecht 2010 Science 328:702-3).
  • 1 Very-high-load activated sludge + settler; 2: Anaerobic digester; 3:
  • Figure 2 shows an embodiment of the system of the second aspect of the invention for main stream treatment, with the next block units: 1 : Very-high-load activated sludge + settler; 2: Anaerobic digester; 3: Granular sludge partial nitritation reactor or biofilm reactor (also called in the present specification as cold ANFIBIO); 4:
  • Granular sludge Anammox reactor Granular sludge Anammox reactor.
  • the closed loop control of the second aspect of the invention is applied to biofilm reactor 3.
  • Figure 3 is a block diagram of the control strategy of the method and system of the invention, to obtain partial nitritation in the aerobic granular sludge reactor (unit 3 in Figure 2) operating in continuous mode.
  • TAN total ammonia nitrogen.
  • SP setpoint.
  • [TAN]sp station calculates the desired ammonium setpoint to keep the adequate concentrations ratio between of ammonium and nitrite.
  • Figure 4 show, by means of two graphs, an experimental demonstration of performance of partial nitritation obtained with the biofilm reactor of the second aspect of the invention, at lab scale.
  • Figure 5 shows a basic layout of the system of the second aspect of the invention, simulated with a model described in the next section, where: 1 : Very-high-load activated sludge + settler. Only considered to determine the buffer capacity (2500 m 3 ) with regard to dynamics of ammonium concentration; 2: Anaerobic digester (not described with the model); 3: Granular sludge partial nitritation reactor (cold ANFIBIO), i.e. the biofilm reactor; volume used in simulations 250 m 3 ; 4: Granular sludge Anammox reactor, volume used in simulations 2000 m 3 . 5: Buffer tank used to regulate the reject water inflow for the biofilm reactor 3.
  • 1 Very-high-load activated sludge + settler. Only considered to determine the buffer capacity (2500 m 3 ) with regard to dynamics of ammonium concentration
  • 2 Anaerobic digester (not described with the model)
  • 3 Granular sludge partial nitritation reactor (cold
  • Figure 6 shows in a graph, for the Scenario A described in the next section, the flow-rates of main stream (imposed to test diurnal variability) and side stream (regulated by the control loop of the system of the second aspect of the invention, to keep the desired ammonium concentration in the biofilm reactor 3).
  • Integrated average of side stream flow-rate yields 2.5 % of the main stream, meaning 35% of the total N treated in the WWTP (Waste Water Treatment Plant).
  • Figure 7 shows, also for the Scenario A, the variability assumed for ammonium concentration in the main stream. Integral ammonium concentration average yields 37.7 glM/rm 3 . The variability is the same for Scenario B, also described in the next section.
  • Figure 8 also associated to Scenario A, shows the effluent of the partial nitritation reactor (cold ANFIBIO, unit 3 in Figures 2 and 5). Note how the control strategy produces an effluent with the adequate ratio between ammonium and nitrite concentrations, as to feed the subsequent anammox reactor (unit 4 in Figures 2 and 5).
  • FIG 9 shows the effluent from the anammox reactor (unit 4 in Figures 2 and 5). Further polishing may include removal of nitrate by heterotrophic denitrification.
  • Figure 10 shows, also for Scenario A, the Ammonium concentration in the cold ANFIBIO reactor (unit 3 in Figures 2 and 5) and ammonium setpoint. Note how in large fraction of the time measurement is very close to setpoint. Flow-rate of main stream has been plotted for direct comparison of the effects on ammonium concentration in the reactor.
  • Figure 1 1 shows the Ammonium concentration in the cold ANFIBIO reactor (unit 3 in Figures 2 and 5) and ammonium setpoint. Flow-rate of side stream and inflow ammonium concentration in the main stream have been plotted for direct comparison of the effects on ammonium concentration in the biofilm reactor 3.
  • Figure 12 shows in a graph, for the Scenario B described in the next section, the flow-rates of main stream (imposed in the scenario to test diurnal variability) and side stream (regulated by the control loop of the system of the second aspect of the invention, to keep the desired ammonium concentration in the reactor).
  • Integrated average of side stream flow-rate yields 1 .0 % of the main stream, meaning 22% of the total N treated in the WWTP.
  • Figure 13 depicts, for Scenario B, the effluent of the partial nitritation reactor (cold ANFIBIO, unit 3 in Figures 2 and 5). Note how the control strategy produces an effluent with the adequate ratio between ammonium and nitrite concentrations, as to feed a subsequent anammox reactor (unit 4 in Figures 2 and 5).
  • Figure 14 also for Scenario B, shows the effluent from the anammox reactor (unit 4 in Figures 2 and 5). Further polishing may include removal of nitrate by heterotrophic denitrification.
  • Figure 15 shows, for Scenario B, the Ammonium concentration in the cold ANFIBIO reactor (unit 4 in Figures 2 and 5) and ammonium setpoint. Note how in large fraction of the time measurement is very close to setpoint. Flow-rate of main stream has been plotted for direct comparison of the effects on ammonium concentration in the reactor.
  • Figure 16 also for Scenario B, shows the Ammonium concentration in the cold ANFIBIO reactor (unit 4 in Figures 2 and 5) and ammonium setpoint. Flow-rate of side stream and inflow ammonium concentration in the main stream have been also plotted for direct comparison of the effects on ammonium concentration in the reactor.
  • the system of the second aspect of the present invention is schematically depicted in Figures 2 and 5, and it includes at least the biofilm reactor 3 (where partial nitritation is performed) integrated in a system including the rest of illustrated units (1 , 2, 4 and 5), said rest of illustrated units belonging or not to the system of the invention, depending on the embodiment, i.e. for an embodiment the system of the invention only comprises the biofilm reactor 3 (and advantageously also unit 5) and is to be integrated in a system comprising the rest of illustrated units, while for another embodiment all the illustrated units are comprised by the system of the second aspect if the invention.
  • the control strategy included in the system and performed by the method of the present invention is illustrated in the block diagram of Figure 3, for an embodiment, were the ammonium closed loop is the one included in the square area indicated as "TAN CONTROL LOOP" and includes a "TAN probe” for measuring the ammonium concentration at the outlet of the reactor 3 (see Figures 2 and 5) to be compared with the ammonium setpoint [TAN] S p, and a "controller” and “pump” which, based on the ammonium setpoint and measurement comparison, acts on the side stream, i.e. on the reject water, entering the reactor 3 (see Figures 2 and 5) in order to control the ammonium concentration in the bulk liquid therein to repress NOB activity and provide an adequate ratio to feed a subsequent anammox reactor.
  • the loop indicated as "[TAN] SP MANAGEMENT” includes the block indicated as
  • NO ⁇ analyzer which on-line measures the sum of nitrite and nitrate concentration in reactor 3, and a "[TAN] S p station” in charge of calculating an varying the [TAN] S p, from inputs received from the "TAN probe” block regarding the ammonium concentration measurements, and from the " NO ⁇ analyzer” regarding the sum of nitrite and nitrate concentration measurements.
  • the manipulated variable will be the flow-rate of the side stream (i.e. reject water, as depicted in Figures 2 and 5).
  • the anaerobic digester 2 will have a discharging buffer tank 5 from which the flow-rate of reject water can be regulated and used for control purposes.
  • the model based study shows the performance of the invention in case of diurnal variability in terms of flow-rate and ammonium concentration of the wastewater.
  • the average flow rate used in the simulations is ca. 2- 10 4 m 3 d "1 , with an average biodegradable COD in the influent of 300 g m "3 (ca.1 - 10 5 p.e).
  • Side stream has been assumed to have a constant ammonium concentration of 1 ⁇ 10 3 g/m 3 .
  • the temperature used for the simulations in all reactors was set to 15°C and a pH of 7.5 was assumed.
  • the influent dynamics may produce a higher demand of side stream for control purposes.
  • Diurnal variations and seasonality may be challenging for the control strategy.
  • BSM1 Benchmark Simulation Model no. 1
  • the pattern imposed is rather extreme, and many WWTP's may have rather less variability, i.e. a lower amount of side stream will be required for control purposes.
  • This diurnal variability in terms of ammonium concentration and flow-rate is used as an example, seasonality or storm events could also be similarly handled by the control strategy.
  • the DO concentration in biofilm reactor 3 ( Figures 2 and 5), could be also manipulated to decrease eventually the conversion of the reactor 3 during low nitrogen-load events. Inflow variations in ammonium concentration will be buffered in the biological reactor 1 removing COD. To take into account this buffering capacity, a volume 2500 m 3 has been considered. The basic layout described with the model as well as the volumes of the reactors considered in the simulations are presented in Figure 5. More details regarding the operating conditions of the reactors are found below, at the end of the present section. Two different scenarios have been considered:
  • Scenario B Existing WWTP's conventionally produce a lower amount of N in the side stream.
  • a potential application of the technology would be the retrofitting of two- stage biological systems (A B plants) (see Wett and Alex, 2003 for a description of an A/B plant).
  • the unit 1 in Figure 4 could be a high loaded A-stage with intermediate clarification and a separate sludge cycle.
  • B stage could be mainly devoted to nitrogen removal through the proposed system (units 3 and 4 as shown in Figure 4). Therefore, in this scenario a side stream with a flow-rate of 1 .0 % of the main stream has been considered, meaning 22% of the total nitrogen. Results are presented in Figures 12-17.
  • a one-dimensional biofilm model was developed to simulate the nitrifying biofilm airlift reactor performance based on Wanner and Reichert (1996) and implemented in the software package AQUASIM (Reichert, 1998), v.2.1 d.
  • the biomass species described as particulate compounds in the biofilm matrix were four in the partial nitritation reactor 3: ammonia-oxidizing bacteria (AOB), nitrite- oxidizing bacteria (NOB), heterotrophic bacteria and inert biomass.
  • Biofilm area was described as a function of the granule radius, to correctly simulate the biofilm geometry (for further details see below Eq. 5).
  • anammox bacteria (AMX) and inert biomass was defined as a function of granule size and number of granules.
  • a detachment rate was used to keep a constant biofilm thickness in steady state at a predefined value.
  • Modeling the TAN control loop One of the key aspects of the development of the mathematical model was to provide a powerful approach able to simulate the control strategy, as described above with reference to Figure 3.
  • the control strategy has two different closed-loops: (i) one to maintain the TAN concentration in the bulk liquid (i.e., the reactor effluent, considering a well-mixed liquid phase in the reactor 3) and, for the embodiment here described, (ii) a second one to control the DO concentration in the bulk liquid.
  • [DO] is the dissolved oxygen concentration in the bulk liquid
  • [DO] S p is the DO concentration setpoint.
  • the setpoint will be kept constant in the range 1 -4 mg/L.
  • the TAN concentration setpoint will be varied on demand depending on the concentration of total nitrogen in the reactor.
  • a ratio of [TAN]/[TNN] between 1.1-1.3 is required to feed the subsequent anammox reactor.
  • An additional measurement of NO ⁇ will be used to estimate the total nitrogen and calculate the adequate TAN concentration setpoint in the so called [TAN] SP station (see Figure 3).
  • the [TAN] SP station calculates on-line the required ammonium concentration depending on the measured NO ⁇ concentration in the reactor
  • Nitrification was defined as a two-step process with a first oxidation of ammonium to nitrite by ammonia-oxidizing bacteria (AOB) and a subsequent oxidation of nitrite to nitrate by nitrite-oxidizing bacteria (NOB).
  • AOB ammonia-oxidizing bacteria
  • NOB nitrite-oxidizing bacteria
  • k(T) k(20°C)e (S1 ) where k is ⁇ , ⁇ , ⁇ or b H and T is the temperature (°C).
  • TAN and TNN were used instead of ammonium and nitrite because they are the true compounds analyzed in the chemical analyses.
  • Eqs. (S6) and (S7) derived from acid-base equilibriums, were used for the calculation of the free ammonia (FA or NH 3 ) and the free nitrous acid (FNA or HN0 2 ) concentrations in equilibrium with TAN and TNN, respectively.
  • Nitrite-oxidizing bacteria N-oxidizing bacteria

Landscapes

  • Life Sciences & Earth Sciences (AREA)
  • Biodiversity & Conservation Biology (AREA)
  • Microbiology (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Health & Medical Sciences (AREA)
  • Molecular Biology (AREA)
  • Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)

Abstract

Selon l'invention, la méthode consiste à effectuer une nitrosation partielle d'eaux usées dans un réacteur à biofilm, en effectuant une régulation en boucle fermée pour réguler la concentration en ammonium dans le réacteur à biofilm en fonction de la concentration en ammonium à la sortie du réacteur à biofilm, et calculer et faire varier la valeur d'une consigne de concentration en ammonium de ladite boucle de régulation fermée en fonction de la concentration en azote à la sortie ou à l'intérieur du réacteur à biofilm. Ce système permet de mettre en œuvre la méthode de l'invention.
PCT/EP2014/071636 2013-10-10 2014-10-09 Méthode et système d'élimination de l'azote d'eaux usées WO2015052279A1 (fr)

Applications Claiming Priority (2)

Application Number Priority Date Filing Date Title
EP13382401 2013-10-10
EP13382401.1 2013-10-10

Publications (1)

Publication Number Publication Date
WO2015052279A1 true WO2015052279A1 (fr) 2015-04-16

Family

ID=49382376

Family Applications (1)

Application Number Title Priority Date Filing Date
PCT/EP2014/071636 WO2015052279A1 (fr) 2013-10-10 2014-10-09 Méthode et système d'élimination de l'azote d'eaux usées

Country Status (1)

Country Link
WO (1) WO2015052279A1 (fr)

Cited By (9)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
CN105254006A (zh) * 2015-10-29 2016-01-20 沈阳建筑大学 一体化半亚硝化厌氧氨氧化装置及其工作方法
CN105461169A (zh) * 2015-12-11 2016-04-06 中国科学院微生物研究所 一种养猪场污水处理工艺
JP2017018876A (ja) * 2015-07-09 2017-01-26 鹿島建設株式会社 有機性廃棄物処理システム及び有機性廃棄物処理方法
WO2017136561A1 (fr) * 2016-02-02 2017-08-10 Microvi Biotech Inc. Nitritation aérobie de l'ammoniac et procédés anammox intégrés
EP3255016A1 (fr) * 2016-06-10 2017-12-13 FCC Aqualia, S.A. Procédé de démarrage et de commande d'un processus biologique d'élimination d'ammonium à de faibles concentrations d'ammonium et à basse température par l'utilisation d'un procédé en deux étapes d'un processus d'élimination d'azote autotrophe
CN109516558A (zh) * 2018-12-17 2019-03-26 桂林理工大学 一种降低污水处理厂运行能耗的方法
CN113072184A (zh) * 2021-04-14 2021-07-06 天朝环境科技(北京)有限公司 基于厌氧氨氧化的独立反硝化“耦合”的系统和水处理方法
CN113885597A (zh) * 2021-10-15 2022-01-04 江南大学 污水处理过程的控制方法、装置、终端及可读存储介质
CN115417493A (zh) * 2022-07-04 2022-12-02 山东臻智行环保科技有限公司 一种描述固定生物膜氨氮降解速率与液相流速关系的模型方法

Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2006142166A (ja) * 2004-11-17 2006-06-08 Kobe Steel Ltd 生物学的廃水処理装置およびその運転制御方法
US20060283796A1 (en) * 2004-03-01 2006-12-21 Kurita Water Industries Ltd. Nitrifying method and treating method of water containing ammonium-nitrogen
US20070175823A1 (en) * 2006-01-31 2007-08-02 Vision Envirotech International Co. Ltd. Sequential batch reactor wastewater treatment process
ES2334321B1 (es) 2009-06-11 2010-12-30 Universitat Autonoma De Barcelona Procedimiento para la nitrificacion parcial en continuo de aguas residuales e instalacion correspondiente.
US20120211417A1 (en) * 2011-02-14 2012-08-23 Xylem Water Solutions Zelienople, Llc Method and System for Controlling Carbon Source Feed to Denitrification Filters
WO2013039582A1 (fr) * 2011-09-16 2013-03-21 Babak Rezania Procédés et appareils permettant d'éliminer l'azote présent dans les eaux usées

Patent Citations (6)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US20060283796A1 (en) * 2004-03-01 2006-12-21 Kurita Water Industries Ltd. Nitrifying method and treating method of water containing ammonium-nitrogen
JP2006142166A (ja) * 2004-11-17 2006-06-08 Kobe Steel Ltd 生物学的廃水処理装置およびその運転制御方法
US20070175823A1 (en) * 2006-01-31 2007-08-02 Vision Envirotech International Co. Ltd. Sequential batch reactor wastewater treatment process
ES2334321B1 (es) 2009-06-11 2010-12-30 Universitat Autonoma De Barcelona Procedimiento para la nitrificacion parcial en continuo de aguas residuales e instalacion correspondiente.
US20120211417A1 (en) * 2011-02-14 2012-08-23 Xylem Water Solutions Zelienople, Llc Method and System for Controlling Carbon Source Feed to Denitrification Filters
WO2013039582A1 (fr) * 2011-09-16 2013-03-21 Babak Rezania Procédés et appareils permettant d'éliminer l'azote présent dans les eaux usées

Non-Patent Citations (18)

* Cited by examiner, † Cited by third party
Title
ABMA WR; DRIESSEN W; HAARHUIS R; VAN LOOSDRECHT MCM: "Upgrading of sewage treatment plant by sustainable and cost-effective separate treatment of industrial wastewater", WATER SCIENCE & TECHNOLOGY, vol. 61, no. 7, 2010, pages 1715 - 1722
ALBERT BARTROLÍ ET AL: "Applying Ratio Control in a Continuous Granular Reactor to Achieve Full Nitritation under Stable Operating Conditions", ENVIRONMENTAL SCIENCE & TECHNOLOGY, vol. 44, no. 23, 1 December 2010 (2010-12-01), pages 8930 - 8935, XP055158341, ISSN: 0013-936X, DOI: 10.1021/es1019405 *
ALEX J; BENEDETTI L; COPP J; GERNAEY KV; JEPPSSON U; NOPENS , PONS MN; ROSEN C; STEYER JP; VANROLLEGHEM P.: "Benchmark Simulation Model no. 1 (BSM1", IWA, 2008
BARTROLI, A.; PEREZ, J.; CARRERA, J.: "Applying ratio control in a continuous granular reactor to achieve full nitritation under stable operating conditions", ENVIRON. SCI. TECHNOL., vol. 44, 2010, pages 8930 - 8935
DE CLIPPELEIR H; VLAEMINCK SE; DE WILDE F; DAENINCK K; MOSQUERA M; BOECKX P; VERSTRAETE W; BOON N: "One-stage partial nitritation/anammox at 15 °C on pretreated sewage: feasibility demonstration at lab-scale", APPL. MICROBIOL. BIOTECHNOL., 2013
HU Z; LOTTI T; DE KREUK M; KLEEREBEZEM R; VAN LOOSDRECHT M; KRUIT J; JETTEN MSM; KARTAL B.: "Nitrogen Removal by a Nitritation-Anammox Bioreactor at Low Temperature", APPLIED AND ENVIRONMENTAL MICROBIOLOGY, vol. 79, no. 8, 2013, pages 2807 - 2812
HU Z; LOTTI T; VAN LOOSDRECHT M; KARTAL B.: "Nitrogen removal with the anaerobic ammonium oxidation process", BIOTECHNOL LETT, vol. 35, 2013, pages 1145 - 1154
JUBANY, I.; CARRERA, J.; LAFUENTE, J.; BAEZA, J.A.: "Start-up of a nitrification system with automatic control to treat highly concentrated ammonium wastewater. Experimental results and modelling", CHEM. ENG., vol. 144, 2008, pages 407 - 419
KARTAL, KUENEN; VAN LOOSDRECHT, SCIENCE, vol. 328, 2010, pages 702 - 3
KARTAL; KUENEN; VAN LOOSDRECHT, SCIENCE, vol. 328, 2010, pages 702 - 3
KARTAL; KUENEN; VAN LOOSDRECHT: "Sewage treatment with anammox", SCIENCE, vol. 328, 2010, pages 702 - 3
PEREZ, J.; COSTA, E.; KREFT, J.U.: "Conditions for partial nitrification in biofilm reactors and a kinetic explanation", BIOTECHNOL. BIOENG., vol. 103, no. 2, 2009, pages 282 - 295
REICHERT, P.: "AQUASIM 2.0-Computer program for the Identification and Simulation of Aquatic Systems", EAWAG, 1998
WANNER, 0.; REICHERT, P.: "Mathematical modeling of mixed-cultures biofilms", BIOTECHNOL. BIOENG., vol. 49, 1996, pages 172 - 184
WETT B: "Development and implementation of a robust deammonification process", WATER SCI. TECHNOL., vol. 56, 2007, pages 81 - 88
WETT B; ALEX J: "Impacts of separate rejection water treatment on the overall plant performance", WATER SCIENCE AND TECHNOLOGY, vol. 48, no. 4, 2003, pages 139 - 146
WETT B; OMARI A; PODMIRSEG SM; HAN M; AKINTAYO O.; GOMEZ BRANDON M; MURTHY S; BOTT C; HELL M; TAKACS , NYHUIS G: "Going for mainstream deammonification from bench to full scale for maximized resource efficiency", WATER SCIENCE & TECHNOLOGY, vol. 68, no. 2, 2013, pages 283 - 289
ZULKIFLY JEMAAT ET AL: "Closed-loop control of ammonium concentration in nitritation: Convenient for reactor operation but also for modeling", BIORESOURCE TECHNOLOGY, vol. 128, 1 January 2013 (2013-01-01), pages 655 - 663, XP055158348, ISSN: 0960-8524, DOI: 10.1016/j.biortech.2012.10.045 *

Cited By (14)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
JP2017018876A (ja) * 2015-07-09 2017-01-26 鹿島建設株式会社 有機性廃棄物処理システム及び有機性廃棄物処理方法
CN105254006A (zh) * 2015-10-29 2016-01-20 沈阳建筑大学 一体化半亚硝化厌氧氨氧化装置及其工作方法
CN105461169A (zh) * 2015-12-11 2016-04-06 中国科学院微生物研究所 一种养猪场污水处理工艺
US20190039926A1 (en) * 2016-02-02 2019-02-07 Microvi Biotech Inc. Aerobic nitritation of ammonia and integrated anammox processes
GB2562965A (en) * 2016-02-02 2018-11-28 Microvi Biotech Inc Aerobic nitritation of ammonia and integrated anammox processes
WO2017136561A1 (fr) * 2016-02-02 2017-08-10 Microvi Biotech Inc. Nitritation aérobie de l'ammoniac et procédés anammox intégrés
US10584047B2 (en) * 2016-02-02 2020-03-10 Microvi Biotech, Inc. Aerobic nitritation of ammonia and integrated anammox processes
GB2562965B (en) * 2016-02-02 2021-09-29 Microvi Biotech Inc Aerobic nitritation of ammonia and integrated anammox processes
EP3255016A1 (fr) * 2016-06-10 2017-12-13 FCC Aqualia, S.A. Procédé de démarrage et de commande d'un processus biologique d'élimination d'ammonium à de faibles concentrations d'ammonium et à basse température par l'utilisation d'un procédé en deux étapes d'un processus d'élimination d'azote autotrophe
CN109516558A (zh) * 2018-12-17 2019-03-26 桂林理工大学 一种降低污水处理厂运行能耗的方法
CN113072184A (zh) * 2021-04-14 2021-07-06 天朝环境科技(北京)有限公司 基于厌氧氨氧化的独立反硝化“耦合”的系统和水处理方法
CN113885597A (zh) * 2021-10-15 2022-01-04 江南大学 污水处理过程的控制方法、装置、终端及可读存储介质
CN115417493A (zh) * 2022-07-04 2022-12-02 山东臻智行环保科技有限公司 一种描述固定生物膜氨氮降解速率与液相流速关系的模型方法
CN115417493B (zh) * 2022-07-04 2023-11-21 山东臻智行环保科技有限公司 一种描述固定生物膜氨氮降解速率与液相流速关系的模型方法

Similar Documents

Publication Publication Date Title
WO2015052279A1 (fr) Méthode et système d'élimination de l'azote d'eaux usées
Miao et al. Enhancing ammonium oxidizing bacteria activity was key to single-stage partial nitrification-anammox system treating low-strength sewage under intermittent aeration condition
Liu et al. Rapid achievement of nitritation using aerobic starvation
Isanta et al. Stable partial nitritation for low-strength wastewater at low temperature in an aerobic granular reactor
Siegrist et al. Anammox brings WWTP closer to energy autarky due to increased biogas production and reduced aeration energy for N-removal
Winkler et al. Modelling simultaneous anaerobic methane and ammonium removal in a granular sludge reactor
De Clippeleir et al. One-stage partial nitritation/anammox at 15 C on pretreated sewage: feasibility demonstration at lab-scale
Ganigué et al. Partial ammonium oxidation to nitrite of high ammonium content urban landfill leachates
CN109996766A (zh) 利用碳源投加进行营养物移除的方法和设备
Bian et al. Achieving nitritation in a continuous moving bed biofilm reactor at different temperatures through ratio control
Jia et al. Effect of organic matter on the performance and N 2 O emission of a granular sludge anammox reactor
Kwak et al. Efficient single-stage autotrophic nitrogen removal with dilute wastewater through oxygen supply control
Kouba et al. The impact of influent total ammonium nitrogen concentration on nitrite-oxidizing bacteria inhibition in moving bed biofilm reactor
Pourbavarsad et al. Nitrogen oxidation and carbon removal from high strength nitrogen habitation wastewater with nitrification in membrane aerated biological reactors
Pan et al. Modeling of the interaction among aerobic ammonium-oxidizing archaea/bacteria and anaerobic ammonium-oxidizing bacteria
Cui et al. Enrichment of comammox bacteria in anammox-dominated low-strength wastewater treatment system within microaerobic conditions: cooperative effect driving enhanced nitrogen removal
Wu et al. Differentiating two partial nitrification mechanisms: inhibiting nitrite oxidizing bacteria activity or promoting ammonium oxidizing bacteria activity
Arora et al. Ecofriendly anaerobic ammonium oxidation system: optimum operation and inhibition control strategies for enhanced nitrogen removal
Murat et al. Performance evaluation of SBR treatment for nitrogen removal from tannery wastewater
Wang et al. Re-configuring mainstream anammox
Park et al. Combination of ion exchange system and biological reactors for simultaneous removal of ammonia and organics
Gao et al. Performance and kinetic process analysis of an Anammox reactor in view of application for landfill leachate treatment
Daudt et al. Assessment of nitrous oxide and carbon dioxide emissions and the carbon footprint in an aerobic granular sludge reactor treating domestic wastewater
Leyva‐Díaz et al. Respirometric method for kinetic modeling of ammonium‐oxidizing and nitrite‐oxidizing bacteria in a membrane bioreactor
Mannina et al. Solids and Hydraulic Retention Time Effect on N2O Emission from Moving‐Bed Membrane Bioreactors

Legal Events

Date Code Title Description
121 Ep: the epo has been informed by wipo that ep was designated in this application

Ref document number: 14789197

Country of ref document: EP

Kind code of ref document: A1

NENP Non-entry into the national phase

Ref country code: DE

122 Ep: pct application non-entry in european phase

Ref document number: 14789197

Country of ref document: EP

Kind code of ref document: A1