EP3891103A1 - Procede de traitement des eaux pour l'abattement simultane du carbone, de l'azote et du phosphore, mis en ?uvre dans un reacteur a film biologique a lit mobile en mode sequentiel discontinu - Google Patents
Procede de traitement des eaux pour l'abattement simultane du carbone, de l'azote et du phosphore, mis en ?uvre dans un reacteur a film biologique a lit mobile en mode sequentiel discontinuInfo
- Publication number
- EP3891103A1 EP3891103A1 EP19816263.8A EP19816263A EP3891103A1 EP 3891103 A1 EP3891103 A1 EP 3891103A1 EP 19816263 A EP19816263 A EP 19816263A EP 3891103 A1 EP3891103 A1 EP 3891103A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- phase
- aerobic
- treatment
- anoxic
- nitrogen
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
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Classifications
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/301—Aerobic and anaerobic treatment in the same reactor
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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
- C02F3/08—Aerobic processes using moving contact bodies
- C02F3/085—Fluidized beds
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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
- C02F3/30—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
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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
- C02F3/30—Aerobic and anaerobic processes
- C02F3/308—Biological phosphorus removal
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/105—Phosphorus compounds
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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
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/14—NH3-N
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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
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/44—Time
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- 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
- TITLE PROCESS OF WATER TREATMENT FOR THE SIMULTANEOUS ABATMENT OF CARBON, NITROGEN AND PHOSPHORUS, IMPLEMENTED IN A BIOLOGICAL FILM REACTOR WITH MOBILE BED IN SEQUENTIAL SEQUENTIAL MODE.
- the invention relates to the field of water treatment, in particular waste water for the purpose of purification.
- the invention relates to a biological process for the simultaneous treatment of carbon, nitrogen and phosphorus in water.
- a cycle of the biological water treatment process in a conventional type free biomass SBR reactor successively comprises the steps of:
- Biological treatment under aerobic conditions allows the degradation of carbon as well as the transformation of ammonium (NH 4 + ) into nitrite ions (N0 2 ) and then into nitrate ions (N0 3 ) (nitrification) thanks to a specific nitrifying biomass.
- Biological treatment under anoxic conditions allows the elimination of nitrate ions (N0 3 ) into gaseous dinitrogen (N 2 ) (denitrification) thanks to a denitrifying heterotrophic biomass.
- the removal of phosphorus can be done either biologically or physicochemically by adding metal salts, such as iron or aluminum salts.
- the biological elimination of phosphorus requires a phase with anaerobic conditions, during which the appropriate biomass releases phosphorus and consumes exogenous carbon to build up internal reserves, and a phase with aerobic and / or anoxic conditions during which even biomass on accumulates a large part of the phosphorus present in the reaction medium thanks to its internal carbon reserves which provide it with the required source of energy.
- Variants of the process described above for optimizing treatment performance are obtained by compartmentalizing the activated sludge SBR reactor. This is then referred to as a treatment process in a compartmentalized type free biomass SBR reactor.
- a treatment process in a compartmentalized type free biomass SBR reactor For example, when extensive denitrification of the effluent is necessary, it is possible to add to the head of the free biomass SBR reactor a compartment used under anoxic conditions and with agitation. This configuration requires the installation of a sequential recirculation of the mixed liquor (free and effluent biomass) using a pump between the head compartment used in anoxic conditions and the other compartment. Recirculation must be stopped, in particular during the decantation and emptying phases of the compartmentalized free biomass SBR reactor.
- the compartment used under anoxic conditions makes it possible to obtain a more efficient biological denitrification of the water to be treated.
- the water to be treated introduced into the head compartment is loaded with COD (Chemical Oxygen Demand), that is to say constitutes an abundant source of carbon, which makes it possible to maintain a high concentration of denitrifying bacteria.
- COD Chemical Oxygen Demand
- This configuration also requires the installation of a sequential recirculation of the mixed liquor (free and effluent biomass) using a pump between the head compartment used in anaerobic conditions and the other (s) compartment (s). Likewise, recirculation must be stopped, especially during the decantation and emptying phases of the SBR reactor.
- a first drawback is that because of the slow settling speed of the suspended matter (consisting mainly of free purifying biomass), these processes require the use of reactors with a large volume.
- a second disadvantage of these free biomass SBR processes is that they have limited treatment performance, in particular limited performance for nitrification. Indeed, the concentration of activated sludge in the SBR reactor is often limited, in practice strictly less than 5 g / L, in order not to alter the clarification step.
- a third drawback of these conventional SBR processes is that it is necessary to maintain a high sludge age in the SBR reactor, in practice a sludge age strictly greater than 15 days at 12 ° C., in order to be able to obtain a level of sufficient nitrification. This implies a considerable increase in the size of the water treatment installations.
- an SBR reactor by alternating anaerobic (s) / aerobic (s) / anoxic (s) phases. It can be used for the treatment of phosphorus in particular.
- the absence of free biomass in the reactor makes it possible to carry out a total or almost total emptying of the liquid contained in the reactor at the end of the SBR cycle and this without prior decantation step, unlike SBR reactors with free biomass or with constituted biomass granules.
- the reactor is fitted with perforated grids which allow the media to be retained in the biological tank while letting the purified water and the suspended matter pass through during the emptying phases. This feature makes it possible to obtain a very compact SBMBBR reactor.
- the treated drained water contains suspended matter, of the order of 100 to 500 mg / L, coming from the water to be treated as well as from the detachment of the surface parts of the biofilm.
- the water treated in an SBMBBR reactor generally requires a step of separation of these suspended solids downstream via a settling tank, a float or a filter.
- the structure used for this separation step can be particularly compact due to the low MES concentrations.
- Tests have been carried out in an SBMBBR reactor on synthetic or semi-synthetic municipal wastewater, using anaerobic / aerobic cycles without limitation of dissolved oxygen, in other words with uncontrolled aeration and therefore at very high concentrations of dioxygen, with KMT and also Kl type supports (cf. HELNESS H., “ Biological phosphorus removal in a moving bed biofilm reactor ”, Trondheim, Norwegian University of Science and Technology, 2007, pages 85-96; Figure 37).
- the Helness results show promising results for the treatment of carbon, nitrogen and phosphorus in the tested waters.
- the inventors of the present invention have repeated these tests on an SBMBBR reactor treating real municipal water, more concentrated in nitrogen than that tested by Helness, without exogenous supply of organic matter and with a COD: NTK ratio of between 5 and 8 (and therefore less favorable for the overall treatment of nitrogen). They were then able to confirm this difference between the time necessary to over-accumulate the phosphorus and to finish the nitrification during the aeration step of the SBMBBR reactor.
- An object of the invention is to propose a method for the simultaneous improved biological treatment of carbon, nitrogen and phosphorus which is simple, flexible, stable and robust and which can be implemented in a particularly compact installation.
- Another objective of the invention is to propose a process which makes it possible to improve the performance for removing total nitrogen and phosphorus by biological means while reducing the organic carbon requirements of the biomass.
- the invention relates to a process for the simultaneous treatment of carbon, nitrogen and phosphorus in water, in a moving-bed biological film reactor in discontinuous sequential mode (SBMBBR), comprising supports capable of developing a biological film. .
- SBMBBR discontinuous sequential mode
- the method comprises successive treatment sequences, each treatment sequence comprising:
- said initial anaerobic treatment phase being followed by at least one aerobic / anoxic cycle consisting of:
- phase in which the biological film is placed, at least locally, in anoxic conditions this phase being concomitant or subsequent to said aerobic treatment phase; the threshold concentration of ammonium ions being calculated to allow the development of anammox microorganisms during the phase in which the biological film is placed, at least locally, in anoxic conditions.
- anobic is meant the presence of oxygen in a reaction medium. The concentration of dissolved oxygen is then generally greater than or equal to 0.5 mg 0 2 / L.
- anaerobic means the total or almost total absence of dioxygen in a reducing reaction medium, that is to say in particular not comprising oxidized forms of nitrogenous compounds, such as nitrates (N0 3 ) or nitrites ions ( N0 2 ) for example.
- nitrogenous compounds such as nitrates (N0 3 ) or nitrites ions ( N0 2 ) for example.
- concentration of dissolved oxygen is then close to 0 mg 0 2 / L.
- “Anoxic” conditions are understood to mean the total or almost total absence of dioxygen dissolved in an oxidizing reaction medium, that is to say comprising oxidized forms of nitrogenous compounds, such as nitrates (N0 3 ) or nitrites (N0 2 ) for example.
- the concentration of dissolved oxygen is then close to 0 mg 0 2 / L.
- anoxic conditions By “locally” anoxic conditions is meant the fact that inside the SBMBBR, there are local zones in anoxic conditions while the SBMBBR is generally aerobic. This takes place in particular in particular embodiments where supports presenting a geometry allowing them to remain very close to each other when the intensity of aeration is moderate, and thus locally form anoxic zones.
- anammox microorganisms is understood to mean microorganisms capable, under anaerobic conditions, of transforming ammonium and nitrite into dinitrogen according to the equation:
- the present invention is therefore based on the implementation in a SBMBBR reactor of a biological treatment having an anaerobic initial phase followed by at least one aerobic / anoxic cycle in which the aerobic phase is implemented so as to create conditions favorable, in particular an appropriate concentration of ammonium ions in the biofilm, for the development of anammox microorganisms under anoxic conditions.
- Anammox microorganisms advantageously allow the elimination of ammonium directly in the form of dinitrogen without passing through the nitrate form (N0 3 ) and without the need for carbon.
- the method according to the invention also allows the development of denitrifying microorganisms capable of accumulating polyphosphates.
- the method according to the invention can in particular be implemented with water to be treated having a relatively low COD compared to their nitrogen and phosphorus content.
- the process according to the invention carried out without adding an external carbon source and / or an external source of metallic salts, can in particular treat water with COD / NTK ratios less than 7, preferably less than 10 (Chemical Oxygen Demand: Nitrogen) Total Kjeldhal).
- COD / NTK ratios less than 7, preferably less than 10
- Total Kjeldahl nitrogen is meant the sum of ammoniacal nitrogen (NH 4 ) and organic nitrogen.
- Biofilm develops on supports adapted to its development. This provides many advantages over free biomass.
- the supports make it possible in particular to obtain a higher concentration of biomass and therefore to reduce the size of the corresponding installations.
- the supports allow an increased selection of the microorganisms of interest, in this case the microorganisms anammox and DPAO.
- the supports also make it easier to obtain a higher sludge age than for an activated sludge process, by allowing microorganisms to develop better.
- the biofilm has a better response to variations in COD and better resistance to possible toxic shocks.
- the phase in which the biological film is placed in anoxic conditions is generally after the aerobic treatment phase.
- the supports are able to remain very close to one another when the aeration is moderate, thus forming local anoxic conditions during an aerobic treatment phase, such as for example the “Z” supports of Anoxkaldnes TM .
- the phase in which the biological film is placed in anoxic conditions can be concomitant or subsequent to the aerobic treatment phase.
- Each treatment sequence of the process according to the invention comprises filling the SBMBBR with water to be treated under anaerobic conditions.
- the filling step of the SBMBBR can be carried out more or less quickly.
- the filling time can in particular be between 30 min to 5 hours and preferably between 90 and 180 minutes.
- the SBMBBR can be more or less filled.
- the SBMBBR has an exchange volume ratio (VER) of between 90% and 100%.
- the exchange volume ratio is defined as the ratio between the volume of water discharged at the end of the cycle by the total volume of water in the SBMBBR after the feed phase.
- the initial phase of anaerobic treatment lasts from 30 min to 5 hours.
- the initial anaerobic phase notably makes it possible to initiate the mechanisms of biological dephosphatation thanks to the presence of DPAO microorganisms.
- Degradation or reduction of the soluble organic carbon in the water present in the SBMBBR reactor and an increase in inorganic phosphorus is observed, the release of inorganic phospore by the DPAO microorganisms being an essential step for the dephosphatation.
- the internal carbon stores built up during the initial anaerobic phase allow POA microorganisms to accumulate polyphosphates using nitrate ions or nitrites ions rather than dioxygen during the at least one aerobic / anoxic cycle.
- the anaerobic treatment phase is followed by at least one aerobic / anoxic cycle, preferably 1 to 5 cycles.
- An aerobic / anoxic cycle includes an aerobic treatment phase. This allows the transformation of ammonium (NH 4 + ) mainly into nitrite ions (N0 2 ) and to a lesser extent into nitrate ions (N0 3 ). So that the transformation of NH 4 + stops mainly at the N0 2 species without being transformed into N0 3 , low concentrations of 0 2 , a limited aeration period, "local" anoxic conditions, as well as a alternation of aerobic / anoxic phase are necessary and are levers to inhibit NOB ("Nitrite Oxydizing Bacteria" which transform nitrites into nitrates) thus allowing to accumulate nitrites.
- NOB Nonitrite Oxydizing Bacteria
- Microorganisms enabling this transformation to take place are, for example, ammonium oxidizing bacteria "Ammonia oxidizing bacteria", or AOB which can transform NH 4 + into N0 2 .
- Ammonia oxidizing bacteria or AOB which can transform NH 4 + into N0 2 .
- NOBs Nirite Oxydizing Bacteria
- the aerobic treatment phase is implemented so as to obtain an ammonium ion concentration greater than a threshold concentration of ammonium ions, this threshold concentration being calculated to allow the development of anammox microorganisms during the phase during which the biological film is placed, at least locally, in anoxic conditions.
- the threshold concentration depends on the COD: NTK: P ratio of the water to be treated.
- the threshold concentration of ammonium ions is> 1 mg N / L, preferably> 2 mg N / L.
- An aerobic / anoxic cycle also includes a phase during which the biological film is placed, at least locally, in anoxic conditions. This phase is concomitant or subsequent to the aerobic treatment phase. During this phase, the anammox and DPAO microorganisms transform NH 4 + , N0 2 and N0 3 into dinitrogen without requiring an external source of carbon. DPAO also ensures the phosphate removal of water by accumulation.
- the at least one aerobic / anoxic cycle lasts from 1 hour to 10 hours.
- each cycle of the at least one aerobic / anoxic treatment cycle, the phase in which the biological film is placed in predominantly anoxic conditions is subsequent to the aerobic phase.
- the ratio between the duration of the aerobic phase and the duration of the phase in which the biological film is placed in predominantly anoxic conditions is advantageously between 1: 1 and 2: 1.
- the duration of the aerobic phase may in particular be 1/2 and the duration of the phase in which the biological film is placed under predominantly anoxic conditions may be 1 / 2, relative to the total duration of the aerobic / anoxic cycle.
- the duration of the aerobic phase may in particular be: 2/3 and the duration of the phase in which the biological film is placed in predominantly anoxic conditions may be 1/3 relative to the duration total aerobic / anoxic cycle.
- the duration of each aerobic phase may in particular be: 1/4 and the duration of each phase in which the biological film is placed under predominantly anoxic conditions may be 1/4 relative to the total duration of aerobic / anoxic cycles.
- the duration of each aerobic phase may in particular be: 1/3 and the duration of each phase in which the biological film is placed in predominantly anoxic conditions may be 1/6 relative to the total duration of the aerobic / anoxic cycles.
- the anaerobic treatment phase lasts from 1 hour to 5 hours and, the at least one aerobic / anoxia cycle lasts from 1 hour to 10 hours.
- the overall soluble nitrogen contents of the water to be treated are mainly ammoniacal nitrogen, the nitrites (N0 2 ) and nitrates (N0 3 ) contents being negligible at the entry of the SBM BBR.
- FIG. 2 is a graph representing the nitrogen concentration of the ammoniacal ion (NH 4 + ) at the inlet of the SBMBBR (mg N / L), the concentration of overall soluble nitrogen (soluble NGL) at the outlet of the SBMBBR (mg N / L ) and the overall soluble nitrogen elimination yield (%) as a function of the days of operation in a process implemented according to the invention where the setting in anoxic conditions is after the aerobic phase.
- the overall soluble nitrogen contents of the water to be treated are mainly ammoniacal nitrogen, the nitrites (N0 2 ) and nitrates (N0 3 ) contents being negligible at the input of the SBMBBR.
- FIG. 3 is a graph representing the nitrogen concentration of the ammoniacal ion (NH 4 + ) at the inlet of the SBMBBR (mg N / L), the overall nitrogen concentration (soluble NGL) at the outlet of the SBMBBR (mg N / L) and the nitrogen elimination yield (%) as a function of the days of operation in a process implemented according to the invention where the setting in anoxic conditions is concomitant with the aerobic phase.
- the overall soluble nitrogen contents of water at to treat are mainly ammoniacal nitrogen, the contents of nitrites (N0 2 ) and nitrates (N0 3 ) being negligible at the input of the SBMBBR.
- FIG. 4 is a graph representing the number of NOB bacteria in the biofilm (ordinate on the left; NOB bacteria / m 2 of support to biofilm) and the number of Anammox bacteria in the biofilm (ordinate on the right; Anammox bacteria / m 2 of support biofilm) depending on the days of testing and for the three implementations of the SBMBBR (conventional implementation on the left, implementation according to the invention where the anoxic conditions are set after the aerobic phase in the middle, implemented according to the invention where the setting in anoxic conditions is concomitant with the aerobic phase on the right).
- FIG. 5 is a graph representing the phosphate concentration (P0 4 ) in the SBMBBR (ordinate on the left; mg P / L), the nitrogen concentration of the ammoniacal ion (NH 4 + ) in the SBM BBR (ordinate on the left ; mg N / L) and the nitrogen concentration of the nitrite ion (N0 2 ) in the SBMBBR (ordinate on the right; mg N / L) during a single treatment cycle which took place during implementation of the SBMBBR process according to the invention where the setting in anoxic conditions is subsequent to the aerobic phase.
- FIG. 6 is a graph representing the phosphate concentration (P0 4 ) in the SBMBBR (ordinate on the left; mg P / L), the nitrogen concentration of the ammoniacal ion (NH 4 + ) in the SBM BBR (ordinate on the left ; mg N / L) and the nitrogen concentration of the nitrite ion (N0 2 ) in the SBMBBR (ordinate on the right; mg N / L) during a single treatment cycle which took place during implementation of the SBMBBR method according to the invention where the setting in anoxic conditions is concomitant with the aerobic phase.
- Tests were carried out according to two embodiments of the invention and compared to the results obtained by another test implementing the "conventional" method in an SBMBBR not forming part of the invention.
- “conventional” supports were used such as, for example, “K5” supports from Anoxkaldnes TM. These supports are perfectly fluidized when the aeration necessary to obtain aerobic conditions is applied.
- Classic SBR cycles include 2 phases: an anaerobic phase followed by an aerobic phase.
- the supports are not sown with anammox batteries before the start of the tests.
- the oxygen contents in the reaction medium, during the aerobic phase are maintained at values between 4 and 5 mg 0 2 / L.
- the reduction in overall soluble nitrogen (soluble NGL) is between 33 and 67%, thus obtaining concentrations of overall soluble nitrogen in the treated water close to 25 mg N / L and always greater than 20 mg N / L over the 600 days of testing.
- the number of NOB bacteria per m 2 of support is high and of the order of 10 9 per m 2 of support. That of Anammox bacteria remains low, of the order of 10 8 per m 2 of support corresponding to the limit of quantification of the analytical method.
- Test 6.2 Implementation of a process according to the invention with the setting up of an anoxic phase after the aerobic phase.
- “Classic” supports were used for this implementation, such as “K5” supports from Anoxkaldnes TM. These supports are perfectly fluidized when the aeration necessary to obtain aerobic conditions is applied.
- the supports were not sown with anammox batteries before the start of the trials.
- SBMBBR substyrene-maleic anhydride-semiconductor
- the processing cycles alternate between an anaerobic phase of 2 hours and an aerobic phase of 6 hours. This period corresponds to a seeding of the biolfilm with dephosphating and nitrifying bacteria.
- an anoxic phase is added after the aerobic phase.
- the duration of the different operating phases is 2 to 3 hours for the anaerobic phase, 4 to 5 hours for the aerobic phase, and 1 to 2 hours for the anoxic phase.
- the aeration conditions (duration and oxygen content) of the aerobic phase are adjusted to reach ammonia (NH 4 + ) contents in the reaction medium greater than or equal to 1 mg N / L before the anoxic phase.
- the oxygen contents in the reaction medium being between 4 and 5 mg 0 2 / L for the aerobic phase, and 0 mg 0 2 / L for the anoxic phase.
- the reduction in overall soluble nitrogen is between 25 and 45% to obtain contents in treated water between 30 and 45 mg N / L.
- the aeration conditions of which are adjusted to reach ammonium (NH 4 + ) contents greater than 1 mg N / L we observe a gradual increase in this reduction which reaches 80% with overall nitrogen contents soluble in the treated water between 10 and 25 mg N / L
- the number of NOB bacteria per m 2 of supports is high and of the order of 10 9 before the 350 th day of operation.
- this number is of the same order of magnitude as for the conventional implementation described in paragraph 6.1.
- the number of NOB decreases to reach a log less. NOB bacteria lose the competition against nitrites against Anammox and DPAOs bacteria and are gradually eliminated from the biofilm.
- the number of Anammox bacteria remains low, of the order of 10 8 per m 2 of support corresponding to the limit of quantification of the analytical method.
- anoxic phase posterior to the aerobic phase, the aeration conditions of which are adjusted to reach ammonium ion (NH 4 + ) contents greater than 1 mgN / L, the number of anammox bacteria gradually increases to 10 11 anammox bacteria / m 2 support. This number of bacteria is considered to be high and representative of a proven activity of the anammox bacteria in the biofilm.
- the overall soluble nitrogen contents are 11 mgN / L, comprising respectively ammonium ion (NH 4 + ) contents of 1 mg N / L of the nitrite ion contents.
- the concentration of P0 4 in the treated water is also less than 0.5 mg P / L, corresponding to a reduction in P0 4 greater than 90% for the cycle in question without adding chemicals.
- the embodiment with an anoxic phase subsequent to the aeration phase is more effective in removing nitrogen than the conventional method.
- the nitrogen elimination yields (soluble NGL) increased rapidly and stabilized at 75-80% over more than 200 days (days 450 to 650 days).
- the content of soluble NGL at the outlet of the reactor decreased significantly to reach less than 15 mg N / L over this same period.
- measurements of Anammox bacteria by qPCR do not make it possible to detect Anammox bacteria (quantities below the limit of quantification of the order of 5.10 8 ). From the implementation of the “anoxia” strategy around day 350, the quantities increased rapidly and significantly for reach values of the order of 1.10 11 .
- the growth and activity of Anammox bacteria largely explains the good nitrogen removal yields.
- “Corrugated” supports were used for this implementation, such as “Z” supports from Anoxkaldnes TM. These supports favoring the creation of anoxic local zones during the aeration phases.
- the operation implemented consists of an anaerobic phase of 2 hours followed by an aerobic phase of 6 hours.
- the dissolved oxygen contents during the aerobic phase being between 4 and 5 mg 0 2 / L.
- supports "Z" by their geometry allow them to remain very close to each other, thus forming local anoxic conditions during the aerobic treatment phase.
- the implementation of the invention comprising an anaerobic phase followed by an aerobic phase during which the concentration of ammonium ions is greater than 1 mg N / L and for which the biological film is placed locally anoxic conditions, we observe a reduction in the overall soluble nitrogen NGL of between 70 and 90% to obtain on average contents in the treated water of the order of 10 mg N / L.
- the average number of NOB bacteria per m 2 of supports is of the order of 10 8 throughout the duration of the tests. Furthermore, the average number of Anammox bacteria per m 2 of supports is of the order of 10 13, that is to say a very high number for a process the treatment objectives of which do not relate exclusively to the reduction of global nitrogen by the bacteria. Anammox.
- the concentration of soluble total nitrogen (NGL) soluble in the treated water has reached 10 mg N / L comprising respectively a concentration of ammonium ions (NH 4 + ) of 0.1 mg N / L, a concentration of nitrites ions (N0 2 ) of 0.9 mg N / L and a concentration of nitrites ions (N0 3 ) of 9 mg N / L.
- the concentration of P0 4 in the treated water is also equal to 0.1 mg P / L, corresponding to a reduction in P0 4 greater than 95% for the cycle in question without adding chemicals.
- Nitrogen content overall soluble (NGL) soluble at the outlet of the reactor fluctuated between 10 and 15 mg N / L with a number of Anamomox bacteria in the biofilm of the order of 10 12 -10 13 / m 2 of support.
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Abstract
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Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
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FR1872437A FR3089512B1 (fr) | 2018-12-06 | 2018-12-06 | Procede de traitement des eaux pour l’abattement simultane du carbone, de l’azote et du phosphore, mis en œuvre dans un reacteur a film biologique a lit mobile en mode sequentiel discontinu |
PCT/EP2019/083345 WO2020114979A1 (fr) | 2018-12-06 | 2019-12-02 | Procede de traitement des eaux pour l'abattement simultane du carbone, de l'azote et du phosphore, mis en œuvre dans un reacteur a film biologique a lit mobile en mode sequentiel discontinu |
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EP3891103A1 true EP3891103A1 (fr) | 2021-10-13 |
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EP19816263.8A Pending EP3891103A1 (fr) | 2018-12-06 | 2019-12-02 | Procede de traitement des eaux pour l'abattement simultane du carbone, de l'azote et du phosphore, mis en ?uvre dans un reacteur a film biologique a lit mobile en mode sequentiel discontinu |
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US (1) | US11820688B2 (fr) |
EP (1) | EP3891103A1 (fr) |
CN (1) | CN113226996A (fr) |
AU (1) | AU2019393988A1 (fr) |
CA (1) | CA3121344A1 (fr) |
FR (1) | FR3089512B1 (fr) |
SG (1) | SG11202105902VA (fr) |
WO (1) | WO2020114979A1 (fr) |
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CN112978902A (zh) * | 2021-03-29 | 2021-06-18 | 国环科技发展(湖北)有限公司 | 一种提标升级mbbr生化处理设备及其方法 |
CN116102166A (zh) * | 2022-12-14 | 2023-05-12 | 北京城市排水集团有限责任公司 | 一种基于微型悬浮载体投加的强化一体化自养脱氮方法 |
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NL1021466C2 (nl) | 2002-09-16 | 2004-03-18 | Univ Delft Tech | Werkwijze voor het behandelen van afvalwater. |
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US20150321937A1 (en) | 2014-05-07 | 2015-11-12 | Veolia Water Solutions & Technologies Support | Method and system for treating wastewater in an integrated fixed film activated sludge sequencing batch reactor |
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CN107010727B (zh) * | 2017-05-22 | 2019-05-03 | 广州大学 | 一种全程低氧曝气sbmbbr同步脱氮除磷方法 |
FR3067024B1 (fr) * | 2017-06-02 | 2020-07-31 | Veolia Water Solutions & Tech | Procede de traitement des eaux dans un systeme comprenant au moins un reacteur sequentiel discontinu et un reacteur a film biologique a lit mobile. |
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WO2020114979A1 (fr) | 2020-06-11 |
US20220017392A1 (en) | 2022-01-20 |
AU2019393988A1 (en) | 2021-06-17 |
CN113226996A (zh) | 2021-08-06 |
FR3089512B1 (fr) | 2020-11-20 |
FR3089512A1 (fr) | 2020-06-12 |
CA3121344A1 (fr) | 2020-06-11 |
US11820688B2 (en) | 2023-11-21 |
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