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
  • C02F3/02—Aerobic processes
  • C02F3/12—Activated sludge processes
  • C02F3/1205—Particular type of activated sludge processes
  • C02F3/121—Multistep treatment
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F3/00—Biological treatment of water, waste water, or sewage
  • C02F3/30—Aerobic and anaerobic processes
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F3/00—Biological treatment of water, waste water, or sewage
  • C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
  • C02F3/348—Biological treatment of water, waste water, or sewage characterised by the microorganisms used characterised by the way or the form in which the microorganisms are added or dosed
• • C—CHEMISTRY; METALLURGY
  • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
  • C02F2301/00—General aspects of water treatment
  • C02F2301/08—Multistage treatments, e.g. repetition of the same process step under different conditions
• • 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 invention relates to a method and a device for the biological treatment of polluted effluents, in particular wastewater, for example urban or industrial waste water, implementing a biomass control within a biological reactor.
• the principle of a biological treatment of pollution consists in providing a pollution-rich raw effluent to a population of bacteria (constituting a biomass) capable of feeding on this pollution to be treated.
• sludge is formed during a biological treatment, and that they include biomass, that is to say the various bacterial populations that have been able to proliferate by feeding on the pollution contained in the raw effluent, and non-degraded pollution particles.
• This document recommends the implementation of a control basin in which accumulate sludge, possibly thickened, obtained by clarification of the outflow of a biological basin.
• the redox potential of this control basin is regulated by acting on an inlet flow in this reactor of this raw effluent to be treated or on a sludge outlet flow from this reactor to the biological basin, so that this potential remains as close as possible to the equilibrium value between an oxidizing state and a reducing state: it follows that reactions involving oxidizing and reducing compounds are thus implemented.
• ONDEO a process for treating wastewater by fixed biological cultures, involving a purification step and a sludge reduction step, these two steps being dissociated.
• the sludge reduction step includes a thermophilic enzymatic degradation step followed by an activated sludge biological treatment step.
• the process also involves sending a fraction of 5 to 25% of the activated sludge into an aerobic "digestion" reactor for 16 to 24 hours before being reinjected upstream of the aeration reactor.
• the known processes are often limited in terms of pollution degradation efficiency, especially when different chemical species are present and some are more difficult to degrade than others.
• the known methods do not allow the recovery of treated organic materials, which is a pity on the economic level.
• the object of the invention is to overcome these disadvantages. It aims for this purpose a method and a biological treatment device implementing an active control on the biomass so as to cause it to consume as much as possible the various kinds of pollution contained in the raw effluent and to produce compounds of interest, without involving significant investment or demanding operating conditions.
• the invention thus proposes a process for the biological treatment of an effluent to be treated containing at least two forms of organic pollution, one of which is more easily biodegradable than the other, using a main aerated biological treatment zone in which the treatment is carried out.
• raw effluent in contact with biological sludge adapted to consume a first form of pollution easier to degrade than a second form of pollution the process being characterized in that at least a fraction of the biological sludge is removed isolated at a distance from the main biological treatment zone, under aeration conditions and time adapted to cause in this fraction a development of new biological functions able to consume the second form of pollution and then recycle at least a portion of this fraction of biological sludge to the main biological treatment area.
• microbiology to monitor the cell viability of the process and the bacterial fauna installed in the biological treatment zone; - enzymology to favor certain beneficial biological reactions.
• the invention thus comprises the combination: a method of metabolic control of sludge within an auxiliary zone, in practice consisting of a reactor called a bioactivation reactor, implementing a recirculation loop between the biological treatment zone and the bioactivation zone; the residence time of the sludge in the bioactivation reactor being defined according to the type of the sludge of the biological treatment zone, such an adjustment being new in itself; and a biomass metabolism management method for degrading particulate pollution by secreting specific compounds (enzymes or the like) and / or by adapting the biomass of the sludge; and by preserving the biomass in this bioactivated (i.e., biologically-modified) state for a suitable time prior to reinjection into the biological treatment zone, this aspect being new in itself.
• a bioactivation reactor implementing a recirculation loop between the biological treatment zone and the bioactivation zone
• the residence time of the sludge in the bioactivation reactor being defined according to the type of the sludge of the biological treatment zone
• the bioactivation zone is aerated, the residence time of the isolated sludge fraction being between 1 and 21 days.
• the bioactivation zone is anaerobic, the residence time of the isolated sludge fraction being defined according to the age of the biological sludge.
• Optional thickening can also be implemented. If the sludge is not thick, it serves to increase the substrate-biomass contact surface. In any case, it can be used to reduce the volume of the pond. A mixer can be used to ensure homogeneity of the sludge if it is thick.
• An optional additional conditioning step may be added for subsequent recovery of interest compounds taken from the outflow from the bioactivation zone to the biological treatment zone, thereby increasing the efficiency of the production of these compounds of interest (in particular: enzymes, biopolymers, etc.) when the objective of the process is focused more specifically for this purpose.
• these compounds of interest in particular: enzymes, biopolymers, etc.
• the existing systems are based on cell lysis and / or solubilization mechanically, thermally or chemically in an auxiliary reactor or not.
• the degradation of the pollution or the production of compounds of interest takes place in a biological treatment reactor (unlike the aforementioned US Pat. No.
• the bioactivation zone makes it possible, because of the fine control and control of the biological phenomena that occur therein, to maintain the sludge contained in the biological treatment zone in an optimum state, in view, after recirculation in the biological treatment reactor, consumption of most of the pollution, including pollution hardly biodegradable, and a transformation of organic matter more important.
• the bioactivation zone is placed downstream of the biological treatment zone and in no case receives the raw effluent since it is desired to induce a nutrient deficiency in this bioactivation zone; the metabolic control of the isolated fraction is thus not based on the redox potential but on other parameters that were not used to follow: soluble chemical oxygen demand (or COD), nitrates, exopolysaccharide content, or enzymatic activities such as ATP (for adenosine triphosphate).
• COD soluble chemical oxygen demand
• nitrates nitrates
• exopolysaccharide content or enzymatic activities
• ATP for adenosine triphosphate
• the activation of the isolated fraction is controlled by biological activity monitoring measures of this isolated fraction (as the case may be: soluble COD content, nitrate content, saccharide content, especially exopolysaccharides, ATP value, etc. ).
• the residence time of the sludge in the bioactivation zone is adapted to the nature of the isolated sludge fraction and can vary from 1 to 48 hours under anaerobic conditions and from 1 to 21 days under anoxic or aerobic conditions.
• the residence time can be set according to the sludge age of the main biological treatment zone: the older the sludge, the longer the residence time in the bioactivation zone.
• the aeration and time conditions are adapted to transform the second form of pollution into valuable products.
• the fraction of biological sludge that is isolated is chosen between 30% and 600% of a daily production of sludge from the main treatment zone or preferably between 30 and 300%.
• the sludge fraction taken can be defined by a predetermined rate with respect to the sludge production of the process, especially during the reference period.
• the aeration and time conditions are defined as a function of the follow-up of at least one parameter characterizing, preferably directly, the biological state of the fraction of isolated sludge, and preferably the state of activity of the the biomass.
• the aeration and time conditions can be predefined or continuously defined.
• this parameter is chosen from a suspended matter indicator (or MES), a soluble or total chemical oxygen demand, a nitrogen species indicator, an enzymatic activity, a protein indicator, a polysaccharide indicator or a composition of biomass.
• the aeration and time conditions are chosen so as to control at least one phenomenon chosen from nutritional deficiency, moderate inhibition, pressure, temperature, pH, a change in nature or concentration of electron acceptors.
• the aeration and time conditions are such that a transformation of at least one form of pollution is continued in the mud fraction isolated between the sampling and the recycling.
• the form of pollution whose transformation is thus pursued may be the first form or the second form.
• At least one subfraction is removed from the fraction which is isolated under aeration conditions and time sufficient to cause the development of other new metabolic functions capable of consuming another form of pollution, and at least a portion of this subfraction is recycled to the biological treatment zone.
• At least a second fraction of the sludge from the biological treatment zone is removed and isolated under aeration conditions and for a time sufficient to cause the development of other new metabolic functions capable of consuming other forms of metabolism. pollution, and at least some of this second is recycled fraction in the biological treatment zone, the first and second sludge fractions being treated in parallel.
• the development of new biological functions includes a proliferation of a biological species, a modification of a distribution of an intracellular enzyme production, a modification of an exo-cellular enzyme emission distribution. or a change in population dynamics of a species.
• a concentration treatment is applied to the fraction before causing in the fraction a development of new biological functions.
• the concentration treatment is applied until a concentration of not more than 40 kg of sludge per m 3 of liquid is obtained in the case where the sludge is mainly composed of mesophilic populations.
• the aeration conditions include an oxygen concentration of less than 2 mg O 2 per liter.
• the invention further proposes, for the implementation of the method defined above, a biological treatment plant for an effluent to be treated containing at least two forms of material or organic pollution, one of which is more readily biodegradable than the the other, the plant comprising a main aerated biological treatment zone in which the raw effluent is brought into contact with biological sludges adapted to consume the first form of pollution easier to degrade than the second, characterized in that it comprises a sampling path for at least a fraction of the biological sludge connected to a secondary zone, the fraction being isolated at a distance from the main biological treatment zone, under aeration conditions and for a time sufficient to cause in this fraction the development of new biological functions able to consume the second form of pollution more difficult to degrade, and a line of r This fraction of biological sludge is recycled to the main biological treatment zone.
• the installation may also include a value chain for products of interest, which may take the form of a product packaging unit for recovery.
• FIG. 1 is a block diagram of a biological treatment plant adapted to the implementation of the invention
• Figure 2 is a diagram of this installation in a particular embodiment
• Figure 3 is a graph showing the evolution over time of the total chemical oxygen demand (abatement). of the COD), soluble COD and polysaccharide content, within the bioactivation reactor of FIG. 2
• FIG. 1 is a block diagram of a biological treatment plant adapted to the implementation of the invention
• Figure 2 is a diagram of this installation in a particular embodiment
• Figure 3 is a graph showing the evolution over time of the total chemical oxygen demand (abatement). of the COD), soluble COD and polysaccharide content, within the bioactivation reactor of FIG. 2
• FIG. 4 is a diagram showing the evolution over time of the nitrogen forms in the
• FIG. 6 is a graph showing the evolution over time of the sludge content (volatile matter in suspension MVS, suspended solids MES and solids DM) within the bioactivation reactor of FIG. 2, FIG. graph showing the evolution over time of the sludge content in the biological treatment reactor of FIG. 2, during the two reference periods, a recirculation period at 30% and a recirculation period at 100%, FIG. 8 is a graph similar to that of FIG. 7, showing the evolution over time of the sludge content in the bioactivation reactor of FIG. 2, during the two reference periods, a 30% recirculation period and a 100% recirculation period, FIG. 9 is a block diagram of another installation according to the invention, comprising several reactors of series bioactivation, FIG.
• FIG. 10 is a block diagram of yet another installation according to the invention, comprising several reactors.
• Figure 11 is a graph of the results obtained with the device of Figure 9
• Figure 12 is a block diagram of yet another installation according to the invention, comprising a conditioning zone between the reactor. bioactivation and the biological treatment reactor
• FIG. 13 is a diagram of another installation conforming to the installation, comprising a conditioning zone at the outlet of a bioactivation reactor.
• the first is a quantitative indicator showing the mass distribution in which the main components Carbon / Nitrogen / Phosphorus are found. It is used to measure particulate organic matter (eg bacteria), mineral matter (eg sands), dissolved salts (containing nitrogen and phosphorus), soluble organic matter (such as proteins or polysaccharides).
• the second is a qualitative indicator of the distribution in danger to health and the environment. It measures endocrine disruptors and heavy metals for example.
• FIG. 1 represents a biological treatment installation 10 comprising:
• a main biological treatment reactor 12 here provided with an air inlet 13 through which the reactor 12 is an aerated reactor (continuous or sequenced aeration, with in this case the presence of time phases adapted to cause an aerobic treatment for carbon and ammonia, then anoxic treatment for nitrates, then anaerobic treatment for phosphorus),
• a concentrator 14 connected, here at the bottom, to an outlet of the biological treatment reactor 12,
• An excess sludge discharge line 19 connected to an outlet of the biological treatment reactor and comprising a pump 20,
• a treated water outlet path 21 connected to an outlet, here at the top, of the biological treatment reactor, and
• an output channel 22 connected to an output of the bioactivation reactor, here at the top and can lead on the one hand to the biological treatment reactor and / or on the other hand to an output of the installation.
• Such an installation makes it possible to implement a method of biological treatment of a raw effluent, capable of controlling the metabolism of the biomass, comprising mainly the following steps: a) an effluent to be treated arriving via the channel 11 is brought into contact with mainly, free cultures forming part of biological sludge, in at least one pond or biological treatment reactor 12; b) a fraction of the sludge of the biological treatment reactor is sent, at a defined rate, to one (or several) bioactivation reactor (s) 15 which is (or are) isolated with respect to the reactor 12 and which can (or can) be individually aerated, or micro aerated (that is, aerated with micrometric size bubbling), or anaerobic, so as to perform biological adaptations of the state of the biomasses of this fraction under the influence of various factors (alone or combined) such as nutritional deficiency, moderate inhibition (ie moderate nutritional deficiency), pressure, temperature, pH , the change of acceptor of electrons (this list not being
• the residence time of the sludge in the bioactivation reactor 15 is controlled by the measurement of parameters representative of the biological state of the sludge isolated therein (suspended solids, nitrogenous forms, soluble and total COD, enzymatic activity, proteins, polysaccharides, composition of biomass, ...) and is specific to each type of sludge.
• the recirculation rate, specific to the treatment in each bioactivation reactor, is a function of the biological state of the biological sludge and the bioactivated sludge.
• a tank located after the bioactivation zone 15 but before returning to the biological sludge basin 12, can be added (see FIG. 12), in order to allow the conservation of the state of the biomass (adapted biological species, specific enzymes , production of products of interest) in a state such that their return to the biological treatment reactor allows further degradation of the organic matter and / or condition the compounds of interest produced in order to be able to value them to another sector .
• a prior step of thickening excess sludge is advantageously carried out in zone 14 by any means allowing the thickening of the sludge (at most 40 kg / m 3 for mesophilic populations).
• the thickening can be done, for example, using a membrane technique, a drip table, a static thickener, a rotary drum, etc.
• the thickening which is optional, serves on the one hand, in the case of non-thick sludge, to increase the substrate-biomass contact surface, and on the other hand, to reduce the volume of the basin.
• a mixer can provide a homogeneity in the case of thickened sludge, but beyond a certain threshold (40 kg / m 3 ), the transfer of oxygen is no longer effective.
• the bioactivation reactor can also work with various families of bacteria such as psychrophiles or thermophiles, for example, by adapting the operating conditions of the reactor.
• the invention can be implemented with any method of biological treatment of polluted effluents and waste.
• the biological treatment can be carried out using conventional processes that remove carbon, ammonium or nitrates, for example activated sludge, BRMs (Membrane BioReactors), or MBBRs (Moving Bed BioReactors). .
• the activated sludge in the case of the example is concentrated between 4 and 40 g / L by decantation (this choice is not imperative) and placed in an aerated column (serving as bioactivation zone) continuously to promote the bacterial growth without nutrient supply.
• the reduced supply of nutrients to the bioactivation reactor causes the bacteria in a state of nutrient deficiency that generates a state of adaptation of the biomass.
• Monitoring of biological parameters and sludge concentration was performed. Monitoring in the bioactivation reactor is based on measurements of soluble COD and nitrates, to which other parameters can be added such as NhU + ion, proteins, exopolysaccharides or cellular activity which allow a continuous analysis and in-situ and thus a control (or command) end.
• the bioactivation reactor 15 is controlled to operate continuously under conditions equivalent to the point of reaching the bearing so that the degradation of the pollutant occurs after recirculation in the effluent treatment biological basin.
• preference is given, in the sludge fraction isolated in the bioactivation reactor, the appearance of bacteria capable of degrading at least one of the forms of pollution present, because not spontaneously degraded in the biological treatment reactor .
• it is advantageous not to allow this new bacterial species to develop within the bioactivation reactor, but to send it to feed in the biological treatment reactor.
• the thickened and activated sludge is recirculated in the upstream biological treatment reactor in order to increase the enzymatic activity within the effluent biological reactor and to allow the solubilization of the pollution which is difficult to biodegrade, thus reducing sludge production. of the system and / or thus increasing the production of interest compounds.
• the recirculated volume is chosen according to the state of the biomass.
• the residence time in the bioactivation zone is predetermined depending on the type of sludge.
• an additional conditioning step may be added for the purpose of conditioning the compounds of interest before recirculation and / or upgrading to another sector.
• Compounds of interest may be activated charcoal, enzymes (eg proteases, carbohydrases, lipases or oxidases), bioplastics, biopesticides and biogas, among others.
• the treated water is an urban wastewater containing 150 mg / L of MES, a total COD of 500 mg / L, a soluble COD of 250 mg / L, a nitrogen concentration (ammonia equivalent) of 35 mg / L , an NGL (global nitrogen) of 50 mg / L, and a phosphorus concentration (phosphate equivalent) of 6 mg / L.
• Screened wastewater 61 is introduced sequentially or continuously into a tank 62 of activated sludge. For example, they are introduced with a continuous flow of 130 L / h.
• the activated sludge tank has a volume of 1100 L. When the tank 62 is not powered by a pump, the water returns in a closed loop to a storage tank.
• An agitator makes it possible to homogenize the incoming effluents with the activated sludge present but must not break the flocs. Fine bubble aeration aerates the mixture to allow bacterial growth as well as decarbonation and nitrification / denitrification processes.
• the sludge between 3 and 5 g / L is discharged to a bioactivation reactor 64, with a volume of between 80 and 350 L.
• the transfer of this sludge from the activated sludge tank to the bioactivation reactor is noted in reference 63.
• the flow transferred to the bioactivation reactor is 44-264 U].
• Excess sludge 66 also leaves the activated sludge tank.
• the sludge treatment rate is 30 to 600%.
• the flat membranes act as clarifiers, that is to say sludge separator of clear water.
• the permeate withdrawn is analyzed for its nitrate content in order to regulate the nitrification / denitritication sequenced.
• An aeration system prevents the clogging of the membranes.
• a volume of activated sludge is sequentially introduced into the bioactivation reactor.
• the sludge is thickened to 20-25 g / L thanks to two immersed membrane modules.
• the permeate withdrawn 67 is analyzed for its nitrate content in order to regulate the sequenced nitrification / denitrification.
• the output flow is 110 L / h and is in sequence mode (8 minutes out of 10), which makes it possible to prevent clogging of the membranes.
• Aeration of large bubbles type at the membranes prevents clogging and aeration fine bubbles at the bottom of the tank allows bacterial growth.
• the imposed conditions depend on the nature of the sludge of the activated sludge basin and allow the increase enzymatic activity.
• this method is implemented so that the biological residence time (that is to say, the residence time in the bioactivation tank 64) is preferably 7 days.
• a slurry volume at 20-25 g / L (item 65) is recirculated daily to the sludge tank activated by a positive displacement pump, so as to degrade the particulate COD and thus reduce the production of sludge.
• the total COD (Dt), the soluble COD (Ds) and the polysaccharides (P) of the sludge placed in aerobic stabilization are monitored as a function of time.
• total nitrogen (Nt), soluble nitrogen (Ns) and nitrates (Ni) were monitored as a function of time.
• the method involves a stabilized biological operation taking into account a repetition of the sampling cycle of a fraction of sludge, its isolation, then its reinjection according to a given recirculation rate.
• FIG. 5 shows the monitoring of the sludge content of the activated sludge basin (the ordinate scale being logarithmic).
• Concentration in MES (Suspended Materials) activated sludge is stable at around 5 g / L. It is the same for the concentration of MS (dry matter) and MVS (volatile matter in suspension).
• MS dry matter
• MVS volatile matter in suspension
• Figure 6 shows the evolution of the sludge content in the bioactivation reactor (there is only one reference period because the activation of the bioactivation was carried out once the activated sludge stabilized).
• the content (representing the various materials contained in these sludges) is stable.
• the concentration of MES is 18 g / L
• the MS concentration is 20 g / L
• the MS concentration is 15 g / L. They are obtained with a thickening process, and are very satisfactory.
• the volume of sludge is decreased, and aeration is nevertheless satisfactory. Subsequently, the recirculation is set up.
• Figures 7 and 8 show respectively the evolution of the sludge in the sludge pool (BA, Figure 7) and in the bioactivation zone (Bl, Figure 8) in different recirculation phases.
• the results show a stability of the concentrations of the two basins: the activated sludge in the main basin is about 6 g / L and the bioactivated sludge in the bioactivation basin at 20 g / L.
• Example 2 Implementation of the Process with Vessels in Series Figure 9 schematically shows an installation 210 similar to that of Figure 1, but comprising several reactors of bioactivation in series, each of them imposing different conditions to promote different enzymatic reactions and thus enrich biodiversity.
• the product or products of the reactions of an upstream reactor are then used as substrates of the reactions of a downstream reactor.
• the carbon is converted into volatile fatty acids, and these are converted into methane or PHA biopolymers.
• each bioactivation reactor there is a reinjection line 217 for each bioactivation reactor. This is a concentrated output (bottom, containing bioactivated sludge). There is also for each reactor a clear (top) outlet, the flow of which can be partially recirculated to reactor 212 (channel 222) if it is desired to control the residence time of certain soluble fractions. differently from the residence time of activated sludge. Finally, a way out of the facility is also provided for each reactor (down).
• the output flow of the reactors 215A and 215B are shared between the following reactor (215B and 215C respectively) and a common reinjection line 217; which can make it possible to vary the proportions of transmission to the next reactor and reinjection.
• FIG. 10 represents an installation 110 similar to that of FIG. 1, except that instead of a single bioactivation reactor, there is one several (115A, 115B, 115C), mounted in parallel, each of them may impose different conditions to promote several different enzymatic reactions and thus enrich the biodiversity, so as to obtain several different products, each of which can to be valued.
• the volatile fatty acids produced can be extracted without being converted into PHA biopolymers.
• FIG. 10 elements similar to those of FIG. 1 are denoted by reference numerals derived from those of this FIG. 1 by adding the number 100; the various bioactivation reactors are labeled 115A, 115B and 115C.
• the recirculation of all or part of the contents of these bioactivation reactors could be provided by the same line, but there is a reinjection line for each reactor 115A to 115C, the lines being numbered 118A, 118B , 118C.
• An exit route out of the facility is provided for each reactor, on the right of the diagram.
• the reactor 115A is conditioned so as to cause the appearance of a biological species capable of consuming the substrates which are difficult to degrade A
• the reactor 115B is conditioned so as to cause the appearance of another biological species capable of consuming the substrates which are difficult to degrade B
• the reactor 115C is conditioned so as to cause the development of a biological species capable of consuming the substrates which are difficult to degrade C.
• This assembly makes it possible to carry out degradations under different bioactivation conditions in the different tanks.
• the environmental conditions are used to promote the enzymatic activity (for example the proteases) and to degrade the material.
• the degradation of the pollution is favored.
• protease yield 0.01 g per gram of carbon At equilibrium, that is to say during the exploitation phase, the production obtained is 230 g per day of PHA biopolymers and 1250 g per day of volatile fatty acids. Recirculation of 2060 g of proteases per day is carried out to promote degradation of the material in the activated sludge basin.
• Figure 11 shows the yields obtained in PHA biopolymers, volatile fatty acids and proteases with and without application of the method, the ordinate values being grams per day. The effect of the process is clearly visible.
• FIG. 12 represents a facility 310 similar to that of FIG. 1, except that an additional conditioning step, referenced 330, which is not mandatory, is added on the reinjection line between the output of the bioactivation reactor 315 and the inlet in the biological treatment reactor 312.
• This conditioning step aims at conditioning the compounds of interest before recirculation and / or upgrading, with the aim of increasing the efficiency of the production of compounds of interest (enzymes, biopolymers, etc.) .
• FIG. 13 represents a similar installation 410, which in this particular case involves a micro-aerated or non-aerated bioactivation reactor 415 producing volatile fatty acids by acidogenesis, according to a fermentation process.
• This reactor 415 is installed in connection with an aerated biological treatment reactor 412.
• the waste water inlet is referenced 411, and a feed path of the bioactivation reactor by the biological treatment reactor is noted 414, and involves a thickening process, or does not involve it.
• the excess sludge leaves the biological treatment reactor via route 420, and the water treated by route 421.
• a separation process referenced 408, is also used, followed by a nitrogen and / or phosphorus precipitation process. These two steps are optional.
• An aerated conditioning bioactivation reactor referenced 409, and comprising two tanks is also used.
• a production of microorganisms 430 capable of accumulating biopolymers is obtained by bioaugmentation, that is to say enrichment of bioorganisms.
• a production of biopolymers 440 is obtained.

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