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WO2015011213A1 - Procédé et système d'amélioration de l'élimination d'azote dans un réacteur biologique séquentiel granulaire (rbsg) et produit-programme informatique - Google Patents

Procédé et système d'amélioration de l'élimination d'azote dans un réacteur biologique séquentiel granulaire (rbsg) et produit-programme informatique Download PDF

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Publication number
WO2015011213A1
WO2015011213A1 PCT/EP2014/065870 EP2014065870W WO2015011213A1 WO 2015011213 A1 WO2015011213 A1 WO 2015011213A1 EP 2014065870 W EP2014065870 W EP 2014065870W WO 2015011213 A1 WO2015011213 A1 WO 2015011213A1
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Prior art keywords
gsbr
ammonium
dissolved oxygen
point
oxygen concentration
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Inventor
Julián CARRERA MUYO
Eduardo ISANTA MONCLÚS
José Luis CAMPOS GÓMEZ
Julio PÉREZ CAÑESTRO
Anuska Mosquera Corral
Ángeles VAL DEL RÍO
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Universidade de Santiago de Compostela
Universitat Autonoma de Barcelona UAB
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Universidade de Santiago de Compostela
Universitat Autonoma de Barcelona UAB
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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
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1263—Sequencing batch reactors [SBR]
    • 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
    • C02F2101/00—Nature of the contaminant
    • C02F2101/10—Inorganic compounds
    • C02F2101/16—Nitrogen compounds, e.g. ammonia
    • 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
    • C02F2209/005—Processes using a programmable logic controller [PLC]
    • 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
    • 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 generally relates, in a first aspect, to a method for enhancing Nitrogen removal in a granular sequencing batch reactor (GSBR), comprising performing said enhancing of Nitrogen removal by controlling the dissolved oxygen concentration (DO) in the GSBR by means of a closed control loop, and more particularly to a method comprising calculating the constant dissolved oxygen concentration set-point value based on the result of an ammonium concentration measurement.
  • GSBR granular sequencing batch reactor
  • a second aspect of the invention relates to a system for enhancing Nitrogen removal in a GSBR adapted for performing the method of the first aspect of the invention.
  • a third aspect of the invention comprises a computer program product, comprising code instructions which when executed in a computer implement the automatic calculation of the dissolved oxygen concentration set-point value according to the method of the first aspect of the invention.
  • GSBR aerobic granular sequencing batch reactors
  • Granules have a compact, dense and thick structure which provides good settling and retention capacities [8 - 9].
  • Granular sludge reactors operate at higher loading rates using more compact reactor designs, if compared with activated sludge [10 - 12].
  • the morphological structure of aerobic granular sludge provides the existence of substrate profiles across the granule depth, enabling simultaneous aerobic and anoxic processes into the same bioparticle.
  • GSBR have shown a very good performance in organic matter and nitrogen (N) removal via simultaneous nitrification and denitrification [10, 13 - 14].
  • a three layer control system of a distributed control system for nitrogen removal in a SBR was disclosed, where the influent quantity, dissolved oxygen (DO), oxidation reduction potential (ORP), pH and temperature were monitored on-line to supervise the course of biochemical reaction. According to the on-line monitoring parameters, the control system adjusted and controlled equipment such as influent pump, blower, mixer, decanter and other electrical equipment.
  • DO dissolved oxygen
  • ORP oxidation reduction potential
  • a Fuzzy control of dissolved oxygen in a SBR pilot plant was disclosed at [37] and compared with classical control techniques (on/off and PID), proving that fuzzy logic was a robust and effective DO control tool, easy to integrate in a global monitoring system for cost managing.
  • the DO control of [37] is aimed to enhancing Nitrogen removal, but is implemented in a system that, contrary to GSBRs, operates according to alternate aerobic and anoxic periods, the DO control not being performed for optimizing the denitrification, as the latter is performed under anoxic conditions.
  • the present invention relates, in a first aspect, to a method for enhancing Nitrogen removal in a granular sequencing batch reactor (GSBR), comprising applying a control strategy for controlling at least part of the process conditions of said GSBR, where said control strategy includes a closed dissolved oxygen concentration control loop with a variable dissolved oxygen concentration set-point and a dissolved oxygen concentration measurement performed at the GSBR, the method comprising establishing at least one constant value for said dissolved oxygen concentration set- point and maintaining said established constant value for at least one operating cycle of the GSBR.
  • GSBR granular sequencing batch reactor
  • the method of the first aspect of the invention in a characteristic manner, comprises on-line measuring the ammonium concentration in the effluent of the GSBR during an operating cycle of the GSBR, preferably at the end thereof, and calculating said constant dissolved oxygen concentration set-point value for a consecutive operating cycle based on the result of said ammonium concentration measurement.
  • said control strategy comprises controlling only said dissolved oxygen concentration, thus constituting a much simpler control strategy than the ones of the state of the art which are based on the control of several process conditions.
  • the method of the first aspect of the invention comprises, for a preferred embodiment, performing the establishing of at least one constant value for said dissolved oxygen concentration set- point by an automatic calculation thereof.
  • the method of the first aspect of the invention comprises establishing an ammonium concentration set-point, having a value that will be lower the nearer the end of the cycle said on-line ammonium concentration measurement is performed, comparing said ammonium concentration set-point with said measured online ammonium concentration and calculating said constant dissolved oxygen concentration set-point value based on the result of said comparison.
  • the method of the first aspect of the invention comprises, for an embodiment, establishing said constant dissolved oxygen concentration set-point value also for assuring a minimum ammonium excess inside the CSBR at the end of the operating cycle.
  • Said minimum ammonium excess is preferentially below 10 mg N-NH 4 + L "1 , more preferentially between 0.5 and 7 mg N-NH 4 + L "1 and even more preferentially substantially equal to 5 mg N-NH 4 + L "1 .
  • the method of the first aspect of the invention comprises, for a preferred embodiment, performing measurements only regarding said dissolved oxygen and ammonium concentration, i.e. without measuring any other parameter.
  • These two variables are easy and commonly measured in GSBRs, thus this preferred embodiment is easily implemented and significantly contributes to the above mentioned simplification of the control strategy for nitrogen removal in comparison with the ones of the state of the art which perform measurements for further variables.
  • the method of the invention comprises performing the on- line ammonium concentration measurement during each GSBR operating cycle and recalculating the constant dissolved oxygen concentration set-point value for the corresponding consecutive operating cycle.
  • the method of the first aspect of the invention comprises establishing a minimum limit value for the dissolved oxygen concentration set-point (such as 2 mg 0 2 L "1 ) which assures granules stability.
  • a second aspect of the invention relates to a system for enhancing Nitrogen removal in a GSBR, comprising control means for controlling at least part of the process conditions of said GSBR that includes a closed dissolved oxygen concentration control loop comprising:
  • a dissolved oxygen concentration measurement unit arranged for performing dissolved oxygen concentration measurements inside the GSBR during an aeration process and with an output connected to a second input of the first comparator for the delivering of the measured values;
  • a first controller with an input connected to an output of said first comparator for receiving an electrical signal result of the comparison of the dissolved oxygen measured and set-point values, and connected or to be connected to oxygen injection means for controlling the oxygen injection inside the GSBR.
  • system of the second aspect of the invention in a characteristic manner, comprises a further closed loop comprising:
  • an ammonium measurement unit arranged for performing ammonium measurements in the effluent of the GSBR during a nitrification process
  • a second comparator with a first input connected to an ammonium set-point, a second input connected to an output of said ammonium measurement unit for the receiving the ammonium measured values, and an output connected to an input of said second controller for the delivering of an electrical signal result of the comparison of the ammonium measured and set-point values;
  • said second controller implements the method of the first aspect of the invention for automatically calculating the at least one constant value for the dissolved oxygen concentration set-point based on the result of said delivered electrical signal.
  • system of the second aspect of the invention further comprises said GSBR.
  • a third aspect of the invention relates to a computer program product, comprising code instructions which when executed in a computer implement the automatic calculation of the dissolved oxygen concentration set-point value according to the method of the first aspect of the invention.
  • Figure 1 Time course concentrations of ammonium, nitrite and nitrate as experimentally measured in the lab-scale GSBR. Experimental data obtained in period A were used for the calibration of the model. Results of the model at the operating conditions established in period C were used to validate the model.
  • FIG. 7 Schematic representation of the effluent concentration of N-species and Nremoval obtained at different DO concentrations.
  • the DO o t value and the DO range with high N-removal efficiency are highlighted with a dotted line and grey band, respectively.
  • FIG. 8 Block-diagram of the cascade control strategy proposed to enhance the Nremoval according to an embodiment of the system of the second aspect of the invention.
  • the primary loop only acts once per cycle, using the ammonium concentration at the end of one cycle (effluent concentration) to establish the DO set-point value of the next cycle.
  • the secondary loop is only active during the aerobic phase of the GSBR cycle, and DO set-point is maintained constant during the whole aerobic phase.
  • Figure 9 DO concentration during aerobic phase, effluent ammonium concentration (end of the cycle) and N-removal efficiencies before and after applying the proposed cascade control strategy in the GSBR.
  • the ammonium set-point was 5 mg N L ⁇ 1 . Since the secondary DO control loop was supposed to be fast and efficient, the represented DO concentration after the control strategy activation is equal to the DO set-point value.
  • FIG. 10 Schematic diagram of the GSBR set-up as implemented with the AQUASIM compartments.
  • a biofilm reactor compartment reactor was connected to a mixed reactor compartment with a high recirculation flow to ensure same bulk liquid concentration of dissolved and particulate compounds. Feeding and discharge operations are performed through the mixed reactor compartment.
  • Figure 11 Example of the effect of applying different reduction factors to the diffusion coefficient of soluble compounds on model COD predictions during the first 60 minutes of a cycle.
  • the reduction factor ( ⁇ 0 ) is only active during the first 3 minutes of each cycle (minute 0 to 3 in the graph), which corresponds to the static (non-aerated) feeding phase of the GSBR.
  • the present inventors realized a study including a mathematical model describing the steady state operation of a GSBR treating diluted swine wastewater which was calibrated and validated with different sets of experimental data. This model was then exploited to assess the impact of easily measurable parameters on the N-removal efficiency.
  • the selected parameters were DO concentration, granule size, NLR and influent C/N ratio. From the results of the exploitation, the above mentioned control strategy to improve the N-removal in GSBRs was proposed and evaluated through modelling.
  • the GSBR operational strategy consisted in stepwise decrease of the dilution ratio of the swine wastewater with tap water.
  • Experimental data from the operational periods A and C from the GSBR were used for modelling purposes.
  • the dilution ratio of swine wastewater with tap water was 1 :25, resulting in an influent composition of 600 mg O2 L ⁇ 1 of readily-biodegradable COD, 60 mg O2 L ⁇ 1 of non-biodegradable COD and 103 mg N L "1 of ammonium (table 1 ).
  • the dilution ratio of swine wastewater with tap water was 1 :15, resulting in an influent composition of 1000 mg O2 L ⁇ 1 of readily-biodegradable COD, 1 16 mg O2 L ⁇ 1 of nonbiodegradable COD and 200 mg N L "1 of ammonium (table 1 ). More details about the performance of the reactor can be found elsewhere [6].
  • Table 1 Experimental data related to the influent composition and biomass characteristics in Periods A and C, used as model inputs to simulate the GSBR operation for the calibration and validation.
  • Non-biodegradable COD (mg 02 L-1 ) 60 116
  • the modelling platform used to develop the mathematical model was AQUASIM [22].
  • the biofilm reactor compartment (based on Reichert [22] mixed-culture biofilm model) provided by AQUASIM was used to simulate the mass transfer and biological conversion processes occurring in the granules.
  • the description of the biofilm in AQUASIM is one-dimensional, and only the perpendicular direction to the substratum is resolved [22].
  • the model included six soluble compounds: oxygen (S02), ammonium (S N H4), nitrite (S N o2), nitrate (SNCH), readily-biodegradable organic substrate (S s ) and nonbiodegradable organic substrate (Si); and five types of particulate compounds: ammonium-oxidizing bacteria (X A ), nitrite-oxidizing bacteria (X N ), heterotrophic bacteria (X H ), storage products (XSTO) and inert particulate organic material (X
  • ASM3 Activated Sludge Model No.3
  • the ASM3 presents several limitations for describing systems operating in batch mode or with nitrite accumulation.
  • two modifications were introduced: (i) the model considered simultaneous growth and storage of organic matter by heterotrophic bacteria as described by Sin et al. [24], (ii) nitrite was included as nitrification intermediate as described by Jubany et al. [25], since there was an evident accumulation of nitrite in the GSBR (Fig. 1 ). Therefore, nitrification becomes a two-step process. Firstly, ammonium is oxidized to nitrite by ammonium-oxidizing bacteria (AOB), and secondly, nitrite is oxidized to nitrate by the nitrite-oxidizing bacteria (NOB).
  • AOB ammonium-oxidizing bacteria
  • NOB nitrite-oxidizing bacteria
  • nitrite was included in the model, all the anoxic processes, heterotrophic and autotrophic, (i.e. AOB and NOB endogenous respiration) were possible either from nitrite or from nitrate [26]. Separate anoxic reduction factors were used for X A , XN and X H [26]. Additionally, the anoxic processes from nitrate had a lower reduction factor to avoid an overall denitrification rate higher than the aerobic consumption rate of COD [26].
  • AOB Ammonium-oxidizing bacteria
  • Nitrite-oxidizing bacteria N-oxidizing bacteria
  • Aerobic growth 0 ⁇ A" ⁇ . . 1 /Y A 0 0 0 1 0 0
  • Nitrite-oxidizing bacteria proceed ⁇ - -1.14/(Y N -
  • Aerobic endogenous respiration 0 -(1-fx) iB-ixrfx 0 0 0 0 -1 f x
  • the biofilm reactor compartment was linked to a completely mixed liquid compartment whose volume can vary during the simulation (Fig. 10; see Vazquez-Padi ' n et al. [20] for further details).
  • the completely mixed compartment received the feeding and effluent withdrawal operations.
  • the biofilm reactor had a constant volume (0.75 L) and contained the total amount of granules and part of the bulk liquid. The rest of the bulk liquid was in the completely mixed reactor compartment (0.76 L). Both compartments were interconnected with a recirculation flow-rate to ensure good liquid mixing.
  • Biofilm area was described as a function of the granule radius, to correctly simulate the biofilm geometry.
  • Total biofilm area was defined as a function of granule size and number of granules (see Jemaat et al. [27] for further details).
  • the granule size used as model input was the volume-weighted average diameter experimentally determined in the lab-reactor. The number of granules was determined dividing the total volume of granules by the volume of a single granule, taking into account the experimentally determined density and total solids concentration.
  • a detachment rate (uDet) was used to keep a constant biofilm thickness in steady state at a predefined value (Eq. 1 ).
  • Period A For the assessment of the N-removal in the GSBR, four relevant and easily measurable parameters at industrial scale (DO concentration, granule size, N LR and influent C/N ratio) were selected, seeking to improve operational strategies. With that purpose, five scenarios were defined: Period A, C/N_Low, C/N_High, NLR_1 .5 and NLR_2.0 (Table 2).
  • Period A scenario presented the characteristics of the GSBR operation in period A.
  • Figs. 2A and 2B The profiles of COD, ammonium, nitrite and nitrate predicted by the calibrated model are shown in Figs. 2A and 2B.
  • COD was consumed (feast phase) and the nitrate remaining from the previous cycle was denitrified.
  • the nitrification became the main biological process.
  • Nitrate was the nitrification product, although a slight accumulation of nitrite occurred from minute 30 to 150 (Fig. 2A).
  • the model was able to correctly describe all the processes occurring during the cycle. First, the COD consumption and subsequent denitrification of the nitrate occurring during the feast phase. And second, the nitrification and nitrate accumulation during the famine phase. Also the nitrite accumulation was adequately predicted by the model, although this accumulation was slightly higher than the experimentally observed. However, the N-total was correctly described by the model.
  • the model did not completely describe the ammonium and nitrite profiles of the famine phase.
  • the model overestimated the nitrite concentrations and underestimated the ammonium concentration (see Fig. 2C).
  • the general trends of both compounds were correctly predicted with the simulation results.
  • the DOo t was 2 and 1 mg 0 2 L “1 for the granule size of 3.5 and 2.0 mm, respectively, and 0.5 mg 0 2 L “1 for the 1 .0 or 0.5 mm, indicating that the DO op t value increased with granule size. Note that for two of the granule sizes (1 .0 and 0.5 mm), the DOopt was obtained at the lowest DO concentration used (0.5 mg 0 2 L "1 ), so the decrease of the Nremoval at DO concentration lower than the DO op t could not be observed, although it probably occurred at lower DO concentrations.
  • the effect of the NLR on the N-removal was also evaluated with the model.
  • One of the advantages of granular reactors is their ability to treat high loading rates due to their high biomass retention capacity [6, 10, 12]. For this reason, the effect of the NLR on the N-removal capacity was studied in two scenarios of 1 .5 and 2-fold higher NLR than that applied in period A, maintaining a constant influent C/N ratio (see Table 2).
  • N-removal according to the granule size.
  • the N-removal efficiency of granules larger than 1 mm decreased with NLR (Fig. 5B).
  • This decrease of N-removal was (4 - 6 %), depending on granule size, but the N-removal efficiency at the DO o t maintained higher than 70% in all cases (Fig. 5B).
  • the N-removal at the DO o t increased with NLR, achieving 80% of N-removal efficiency at in the NLR_2.0 scenario. Therefore, in case of an increase of NLR, the lower the granule size, the better the achieved N-removal. Nevertheless, if the DO concentration is maintained at a value close to the DO o t, good N-removal efficiencies could be obtained independently of the granule size.
  • a control strategy was proposed based on determining the DO concentration ensuring a slight excess of ammonium at the end of each GSBR cycle, which have been found the key to achieve high N-removal efficiencies.
  • the proposed control strategy had a cascade control structure, with a primary control loop of ammonium concentration at the end of the cycle, and a secondary control loop of DO concentration along the aerobic phase of the GSBR (Fig. 8).
  • the secondary loop comprises:
  • a dissolved oxygen concentration measurement unit DOm arranged for performing dissolved oxygen concentration measurements inside the GSBR during an aeration process Pa and with an output connected to a second input of the first comparator DOm for the delivering of the measured values;
  • C1 for receiving an electrical signal result of the comparison of the dissolved oxygen measured and set-point values, and connected or to be connected to oxygen injection means V (such as an Air-Flow valve) for controlling the oxygen injection inside the GSBR.
  • oxygen injection means V such as an Air-Flow valve
  • the primary loop comprises:
  • an ammonium measurement unit Am arranged for performing ammonium measurements in the effluent of the GSBR during a nitrification process Pn by means of which ammonium is obtained as outcome;
  • a second comparator C2 with a first input connected to an ammonium set-point N-NH4sp, a second input connected to an output of said ammonium measurement unit Am for the receiving the ammonium measured values, and an output connected to an input of said second controller U2 for the delivering of an electrical signal result of the comparison of the ammonium measured and set-point values.
  • the second controller U2 implements the method of the first aspect of the invention for automatically calculating a constant value for the DO concentration set- point based on the result of said electrical signal delivered by the second comparator C2.
  • the manipulated variable of the primary control loop was, consequently, the DO set-point of the secondary loop [33].
  • the particularity of this control strategy was that the primary ammonium control loop would only act once per cycle. Therefore, after measuring the ammonium concentration at the end of the cycle, the control loop would establish the DO set-point for the next cycle.
  • the ammonium set-point for the primary loop was set to 5 mg N-NH4 + L "1 . This set-point was justified by the precision of the current on-line ammonium measurement devices, but also by the importance of having enough range to measure the error between the online and set-point ammonium concentrations, in order to calculate the control action (Fig. 7).
  • DO concentration in the reactor should be sufficiently close to the value of DO o t as to obtain high N-removal efficiencies when using 5 mg N-NH 4 + L "1 as ammonium set-point.
  • the short term effectiveness of the proposed control strategy over the N-removal efficiency was simulated with the model using the conditions applied in Period A with a granule size of 2 mm.
  • a proportional (P) controller was used [33].
  • the gain of the P controller was set to 0.25 mg 0 2 mg "1 N-NH 4 + .
  • the secondary control loop (Fig. 8) was assumed to have a fast response because the control of DO in the model was described with a high gas-liquid oxygen transfer rate (see the details in SI and Jemaat et al. [27]).
  • the model was run until steady state with a DO concentration of 4 mg 0 2 L "1 , obtaining complete nitrification at the end of the cycle and 48% of N-removal efficiency (see Fig. 9). Then the control strategy was activated. During the first 36h after the control activation (12 cycles) the primary ammonium control loop progressively reduced the DO set-point of the secondary DO control loop, until 1 mg 0 2 L "1 . At that DO concentration, ammonium concentration started to accumulate for the first time in the effluent (Fig. 9).
  • [DO] is the dissolved oxygen concentration in the bulk liquid
  • [DO]SP is the DO concentration set-point (Jemaat et al., 2013).
  • N-removal was enhanced when a small excess of ammonium was maintained in the effluent, i.e. at the end of the GSBR cycle (i.e. 5 mg N- NH4+ L-1 ). • The required ammonium excess was easily achieved by imposing the adequate DO concentration in the reactor, to limit the nitrification step.
  • the control strategy will set the appropriate DO set-point at whatever values of granule size, influent C/N ratio or NLR. Therefore a high N-removal will be assured by the control strategy against disturbances in those variables, which are common during the reactor operation.

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Abstract

La présente invention concerne un procédé et un système d'amélioration de l'élimination de l'azote dans un réacteur biologique séquentiel granulaire (RBSG) et un produit-programme informatique. Le procédé consiste à appliquer une stratégie de contrôle comprenant une boucle de contrôle de l'oxygène dissous (OD) fermée ayant un point de consigne de concentration en OD variable et une mesure de la concentration en OD réalisée au niveau du RBSG, à mesurer en ligne la concentration en ammonium dans l'effluent du RBSG pendant un cycle de fonctionnement du RBSG et à calculer une valeur de point de consigne de la concentration en OD constante pour un cycle de fonctionnement consécutif sur la base du résultat de ladite mesure de concentration en ammonium. Le système est conçu pour mettre en œuvre le procédé de l'invention. Le produit-programme informatique comprend des instructions de code pour le calcul automatique de la valeur de point de consigne de la concentration en OD.
PCT/EP2014/065870 2013-07-24 2014-07-24 Procédé et système d'amélioration de l'élimination d'azote dans un réacteur biologique séquentiel granulaire (rbsg) et produit-programme informatique Ceased WO2015011213A1 (fr)

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CN108473349A (zh) * 2016-01-12 2018-08-31 奥加诺株式会社 颗粒形成方法和废水处理方法
WO2018215561A1 (fr) 2017-05-23 2018-11-29 Haskoningdhv Nederland B.V. Nitrification et dénitrification simultanées régulées dans le traitement des eaux usées
EP3757074A1 (fr) 2019-06-26 2020-12-30 Fundación Centro Gallego de Investigaciones del Agua Procédé d'élimination d'azote à partir d'eaux usées dans un réacteur discontinu séquentiel comportant une biomasse granulaire aérobie
CN114804340A (zh) * 2022-04-28 2022-07-29 北京工业大学 一种在污水生物处理过程中利用聚赖氨酸保留氨氮的方法
CN116718742A (zh) * 2023-05-06 2023-09-08 四川文韬工程技术有限公司 一种未建污水厂地区的水质组分分析方法
CN117247132A (zh) * 2023-11-15 2023-12-19 成都之维安科技股份有限公司 一种基于aao工艺的智能精准曝气方法

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