WO2006114552A2 - Procédé d'épuration d'effluent en réacteur anaérobie - Google Patents
Procédé d'épuration d'effluent en réacteur anaérobie Download PDFInfo
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- WO2006114552A2 WO2006114552A2 PCT/FR2006/050392 FR2006050392W WO2006114552A2 WO 2006114552 A2 WO2006114552 A2 WO 2006114552A2 FR 2006050392 W FR2006050392 W FR 2006050392W WO 2006114552 A2 WO2006114552 A2 WO 2006114552A2
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- reactor
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- process according
- purification process
- microorganisms
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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
- C02F3/28—Anaerobic digestion processes
- C02F3/2806—Anaerobic processes using solid supports for microorganisms
-
- 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
- Y02E—REDUCTION OF GREENHOUSE GAS [GHG] EMISSIONS, RELATED TO ENERGY GENERATION, TRANSMISSION OR DISTRIBUTION
- Y02E50/00—Technologies for the production of fuel of non-fossil origin
- Y02E50/30—Fuel from waste, e.g. synthetic alcohol or diesel
Definitions
- the invention relates to a process for purifying effluent in anaerobic reactor. More specifically, the invention relates to a purification process in which the microorganisms are fixed on solid supports and form a fixed bed, or anaerobic filter that can be fluidized demand. The invention also relates to the use of a biological reactor in which the carriers carrying the microorganisms are allowed to organize in a fixed bed during the stationary operating phase. The supports are suspended only during the initial phase of reactor overload (start-up phase) or punctually during the stationary operating phase only once the reactor is clogged.
- the invention relates to the purification of wastewater by anaerobic treatment.
- aerobic reactors for the treatment of heavily loaded wastewater results in the production of significant amounts of sludge by the microorganisms to clean up the wastewater.
- an average of 50% of the pollutants eliminated in the aerobic reactor are converted into sludge, which is another form of pollution that will in turn have to be treated.
- Aerobic processes are therefore used primarily for effluents with little concentration in pollution.
- aerobic reactors require frequent and prolonged aeration, consuming energy.
- biomass we mean all the microorganisms used to degrade the pollution contained in the effluent.
- biofilm we mean highly structured cellular formations, in which microbial cells, which serve to degrade the pollutants contained in the effluent, which are included in a complex matrix.
- the effluent to be treated flows through the support from the bottom up (upflow) or from the top down (downflow).
- the effluent is thus in contact with the biomass which carries out the depollution.
- the two main disadvantages of such an anaerobic biological reactor are, on the one hand, as for any anaerobic process, the length of the reactor startup phase, which usually lasts between 3 and 6 months, and on the other hand the risk of clogging of the reactor which may cause, after a longer or shorter time, a total blockage of the reactor.
- the length of the reactor startup phase which usually lasts between 3 and 6 months
- the risk of clogging of the reactor which may cause, after a longer or shorter time, a total blockage of the reactor.
- sludge production by microorganisms is less important in this type of reactor than in aerobic reactors, over time the sludge accumulates on the walls of the supports and in the interstices between the supports and can not not be evacuated. The accumulation of sludge can result in reactor service by blocking it completely.
- a biological reactor using fixed supports on whose walls the microorganisms are fixed.
- the supports are formed of hollow tubes fixed at one end and in an orderly manner in the reactor vessel.
- the tubes have a diameter of 102.5 mm and are divided in their diameter into fourteen channels in which the microorganisms are fixed and can thus be organized into biofilm.
- an anaerobic reactor operating in a fluidized bed, that is to say with permanently movable supports.
- the microorganisms are fixed on supports of very small sizes maintained in suspension in the reactor.
- the supports are movable in the reactor and rub against each other and / or with the internal walls of the reactor vessel, tearing the biofilm formed by the microorganisms as soon as it exceeds a certain thickness.
- the sludge falls into the bottom of the tank where it can be purged or exit with treated effluent. There is thus no risk of clogging of the reactor since the accumulation of sludge in the supports is made almost impossible.
- the permanent or quasi-permanent mobility of the supports is obtained by the creation of permanent or quasi-permanent turbulence in the reactor.
- An object of the invention is to treat effluents by biological treatment in an anaerobic medium, so as to eliminate a large part of the pollution they contain with excellent performance, without the risk of clogging the reactor, with low costs and low operating time, and with a sharp reduction in the duration of the initial phase of ramp up of the reactor (phase starting).
- the increase in load is the gradual increase in the load applied over time following the seeding of the reactor, until the nominal load which has been set during the design of the reactor is reached.
- Another object of the invention is to allow the treatment of all types of effluents, including effluents heavily charged with pollution.
- a further object of the invention is to promote the growth of biomass in the reactor.
- the invention also aims to provide a solution for the treatment of effluents, which is easily used directly by polluting industries.
- the invention proposes to treat the wastewater to be decontaminated in an anaerobic reactor, in a fixed bed, which can be made mobile according to the needs of the users, during the start-up phase or the unclogging phase of the reactor, in order to optimize its operation.
- Fixed bed operation results in low costs and ease of operation.
- the fixed bed is formed of a plurality of supports arranged in bulk in the reactor and on which the microorganisms form a biofilm and accumulate in the supports and in the interstices created between the supports.
- the growth of the biofilm on the supports is favored by maintaining short dwell times.
- the frequent fluidization of the supports can also promote the formation of the biofilm.
- the aim is to reduce the duration of the rising phase by removing free bacteria from the reactor to force the fixing on the supports.
- a second step (stationary operating phase), the reactor operates in a fixed bed at its nominal load.
- the retention of interstitial biomass is then favored.
- Interstitial retention refers to the accumulation of biomass in interstices of supports and between supports.
- the fluidization device is no longer used and the reactor operates in pure fixed bed. It is in this way that we manage on the one hand to mount high load in a short time, usually less than a month, and on the other hand to achieve very important loads for a fixed bed, it that is, up to 45 kg COD / m3.
- As fixed-bed reactor wastewater treatment is used, sludge accumulates on, in, and between supports, and begins to clog the reactor. When the reactor is at least partially clogged, it is provided according to the invention to fluidize the supports.
- the fluidization is temporary and spread over a short time, that is to say of the order of a few minutes or a few hours.
- the mobility of the supports allows sufficient friction to drop the sludge in the bottom of the tank.
- the surplus sludge can then be removed from the tank in a conventional manner.
- the fluidization is then stopped.
- the carriers become immobile again in the reactor so as to form a fixed bed again.
- the time flowing between two fluidizations can be relatively long, of the order of several months to several years, depending on the type of media and the load applied.
- the subject of the invention is therefore a process for purifying an effluent in anaerobic reactor in which the microorganisms are retained by supports, the supports forming a fixed bed in a portion of the reactor, characterized in that it comprises the step of temporarily suspending the supports in the entire reactor or, during the start-up phase, for eliminating the free or trapped microorganisms in or between the supports or, during the stationary operating phase, for unclogging of the reactor once it is at least partially clogged.
- Purification means at least partial removal of pollution contained in the effluent at the time of entering the reactor.
- Suspending consists of making the initially immobile supports mobile in the reactor. The supports can then be distributed throughout the reactor volume and move. Suspending is only temporary insofar as, as soon as the unclogging stops, the supports reorganize into a fixed bed.
- the effluent purification process comprises the following steps: a) carrying out a reactor overload with a hydraulic residence time (TSH) of less than 48 hours; b) purify the effluent by maintaining the supports in a fixed bed; c) fluidizing the reactor once it is at least partially clogged, by temporarily suspending the supports.
- TSH hydraulic residence time
- Raising the reactor load means the reactor initiation phase, during which the applied load is regularly increased to the nominal load defined during the design and where it is aimed at the formation of biofilm on the supports.
- the reactor is loaded up to 20 kg COD / m3, +/- 10%.
- This step of loading is characterized by a gradual increase in the COD of the effluent passing through the reactor, with a short hydraulic residence time during the entire stage of increase in load, so as to increase the applied load of the reactor .
- the COD of the effluent to be treated, and therefore the load applied is increased daily by a constant percentage and between 5 and 15%.
- the daily increase can be 10% of the previous value.
- Applied charge means the amount of pollution that is treated in the reactor per cubic meter of reactor (applied volume load) or per gram of biomass (applied mass load) per day.
- the TSH is between 12 and 36 hours, preferably between 20 and 30 hours, and even more preferably between 22 and 26 hours, more preferably equal to 24 hours.
- step a) lasts 35 days, plus or minus 5 days.
- the supports are put at least once in suspension; for example, the supports are temporarily suspended for 10 minutes, +/- 2 minutes, every hour; it is also possible to provide a continuous suspension throughout step a).
- Step b) lasts between 2 and 12 months, preferably between 6 and 9 months, even more preferably 8 months.
- the purification step b) is prolonged as long as the reactor is not clogged, and the purification efficiency, for an applied volume load (OLR) corresponding to the nominal load, is satisfactory.
- OLR applied volume load
- the treatment efficiency is satisfactory when it is at least equal to 80%.
- the threshold value is set at 75% of treatment efficiency.
- Step c) unclogging lasts between 15 minutes and 1 hour, plus or minus 10 minutes. Once the reactor unclogged, it ceases the suspending of the supports, so that they reorganize into a fixed bed, can then again proceed to the purification of the effluent according to step b), and so to after.
- the supports comprise attachment zones on which the microorganisms can be fixed, the attachment zones being arranged to allow a physical retention of said microorganisms.
- the attachment zones comprise fins. The microorganisms can then be fixed on said fins, and form a biofilm, and / or be retained in interstices between the fins and / or between the supports, in which they accumulate.
- These supports are preferably extruded or molded and provided with internal fins protected turbulence that may exist within the reactor, said inner fins having a significant attachment surface for microorganisms. These supports make it possible to fix the biomass on a large surface but in addition to retain the biomass in the interstices between the fins and between the supports themselves.
- the means for fluidizing the supports may be located in a portion of the reactor without the fixed bed.
- the means for supplying the reactor vessel with effluent can be located in the part of the reactor that does not have a fixed bed. It is also possible to provide homogenization means for distributing the effluent in the assembly of the reactor.
- the supports occupy between 40% and 80% of the reactor volume and preferably between 50% and 70%.
- the fluidization can be obtained by operating a fluidization system, such as a pump, capable of creating turbulence inside the reactor, so as to suspend the supports.
- a fluidization system such as a pump
- fluidization system may be removable and external to the reactor, said fluidization system being connected at least temporarily to pipes to perform the unclogging.
- external fluidization system it should be understood that the fluidization system is not immersed in the reactor volume but is located outside. The fluidization system is therefore not in contact with the effluent and the supports. This facilitates in particular the maintenance of the fluidization system which is in fact easily accessible.
- the fluidization of the supports in stationary operation is carried out only once that the reactor is clogged.
- the time required for clogging may vary from one reactor to another, depending in particular on the type and quantity of supports, the amount of biomass in the reactor and the applied load.
- the declogging can be periodic, with a period ranging from a few days to a few years depending on the needs.
- the declogging can be performed once a year, or every two years, three years, and so on. Unclogging can also take place irregularly, each time the reactor is more or less clogged and the user wishes to unclog it.
- the supports are reorganized into a fixed bed.
- the invention also proposes a use of a biological reactor comprising microorganisms retained on supports and fluidization means capable of suspending the supports, characterized in that the reactor is used for the purification of an effluent by treatment. anaerobic, the fluidization means being used temporarily to unclog the reactor, the supports being immobile and forming a fixed bed in the reactor when the fluidization means are not used.
- the supports occupy for example
- the supports 40% to 80% of the reactor volume, and preferably 50% to 70%, so that when the temporary fluidization means are used the supports can be distributed throughout the reactor volume, because of the suspension said supports which allows them to be mobile in the reactor volume.
- the supports used are for example extruded or molded and provided with fins, the microorganisms being fixed on said fins and / or retained in interstices between the fins and / or between the supports.
- the fluidization means of the biological reactor used comprise a fluidization system capable of creating turbulence inside the reactor, to suspend the supports.
- the fluidization system is for example a pump.
- the pump may be a water pump or a biogas pump.
- the fluidization system comprises a reserve of inert gas, such as a nitrogen cylinder, from which the pressurized gas is injected into the reactor.
- a reserve of inert gas such as a nitrogen cylinder
- the fluidization system may be located outside or inside the reactor.
- said fluidization system also comprises at least one pipe, said pipe opening into the reactor.
- FIG. 1 an example of a biological reactor that can be used for the treatment of effluents according to the invention
- FIG. 2 a second example of a biological reactor that can be used for the treatment of the effluents according to the invention
- 3 a representation of the biological reactor according to FIG. 2, in which the supports are fluidized;
- FIGS. 4A and 4B a schematic representation of a biomass fixation support, seen from the side ( Figure 4A) and seen from above ( Figure 4B);
- FIG. 5 a graphical representation of the evolution of the hydraulic retention time (TRH) and the amount of pollution (OLR) introduced into the reactor in an exemplary implementation of the treatment according to the invention
- FIG. 6A and 6B graphical representations of the evolution of the efficiency of the effluent treatment process as a function of the hydraulic retention time (TRH) and the amount of pollution (OLR) introduced into the reactor;
- FIG. 7 a graphical representation of the increase in load in a reactor used according to the invention.
- FIG. 8 a graphical representation of the evolution of the charges applied in a reactor as a function of the supports used.
- FIG. 1 shows a biological reactor 1 capable of operating anaerobically.
- the reactor 1 comprises a tank 2 in which a plurality of solid supports 3 are arranged in bulk.
- the supports 3 have a density substantially lower than the density of the water so that all the supports are concentrated in an upper portion 4 of the vessel 2 of the reactor 1.
- the density of the supports is for example between 0.90 and 1, 2.
- FIGS. 4A and 4B show an example of support 3 that can be used in reactor 1.
- Support 3 has a generally cylindrical circular shape with a height h of about 3 cm and a diameter d of between 2.5 and 3, 5 cm. By height h is meant the dimension of the support 3 in the direction parallel to the longitudinal axis of the support.
- the support 3 is provided with a plurality of rigid fins 11 directed towards the center 12 of the support 3.
- the fins 11 are all fixed by a first end 15 to a first rigid ring 13 and by a second end 16 to a second ring Rigid 14.
- the fins 11 form the body of the support 3.
- the fins 11 are spaced apart from each other so as to provide a space 17 through which the effluent, or the liquid in general, can pass in order to be in contact with the part of the fins 11 directed towards the center 12 of the support 3.
- the supports 3 used are supports of macroscopic size, with a height h of between 15 mm and 50 mm, and with a diameter of between 10 mm and 50 mm.
- fluidizing means 6 Internal, that is to say fully housed in the tank 2.
- the fluidization means 6 comprise a pump 7 adapted to blow a gas or a liquid in the tank 2.
- the pump 7 can be actuated and stopped on demand.
- the lower part 5 of the vessel 2 of the reactor 1 also comprises homogenization means 8.
- the homogenization means 8 comprise, for example, a turbine provided with blades so as to mix the effluent which enters the vessel 2 at the level of the lower part 5 of said tank 2.
- Such homogenization means 8 may be particularly advantageous when the reactor 1 is used to treat highly charged effluents, which otherwise could remain concentrated locally in the lower part of the tank 2.
- the effluent is mixed with the rest of the fluid contained in the vessel 2.
- the effluent thus passes through the upper part 4 of the vessel 2 containing the fixed bed formed by the supports 3.
- a gate located at the outlet of the liquid prevents the supports 3 from leaving the tank 2 through the tank outlet pipe (not shown) through which the treated effluent is discharged.
- the fixed bed formed by the supports 3 is located in the lower part 5 of the tank 2.
- the effluent then enters the tank 2 at the top 4, or the bottom 5, which may also include the homogenization means 8 and the fluidization means 7.
- the fluidization means 6 may be located in the part of the reactor 1 comprising the fixed bed.
- the fluidization means 6 are only partially internal.
- the fluidization means 6 comprise a pump 7 external to the tank 2 and an internal pipe system 9.
- the pump 7 is connected to the pipe system 9 located inside the tank 2.
- the pipe system 9 comprises a plurality of pipes distributed in the bottom 10 of the tank 2. It is of course possible to provide only a single pipe in the piping system 9.
- the external pump 7 may be a removable pump. Thus, it is possible to connect the pump 7 to the pipe system 9 temporarily when the user wishes to create turbulence in the tank 2.
- FIG. 3 one can see the biological reactor 1 in which the fluidization means 6 have been activated.
- the pump 7 blows a liquid or a gas into the tank 2, so that turbulence is created.
- the turbulence is sufficient to disorganize the fixed bed supports 3.
- the supports 3 are all suspended in the entire volume of the vessel 2, moving in said tank 2. Thus, the surplus sludge accumulated in the supports 3 can fall into the bottom of the tank, where it can be easily drained.
- the decoupling applied load / hydraulic residence time is achieved by initially decreasing the concentration of COD in the inlet effluent, that is to say by diluting the latter, and increasing it gradually until reaching the concentration in COD of the raw effluent to be treated.
- the COD of the effluent to be treated is preferably increased daily by a constant percentage and between 5 and 15%.
- the concentration of COD in the effluent is increased by approximately 10% every day, which makes it possible to pass from a COD of the feed of 0.5 to 20 kg. / m 3 in 35 days.
- the TSH being 24h during these 35 days, we obtain at the end of this period a
- the hydraulic residence time is constant.
- a short residence time preferably less than 48 hours, and variable. For example, during the first 10 days of the scaling step, one maintains a
- TSH 24 hours, then for the next 10 days a TSH is maintained
- the applied load can be increased, up to most often greater than or equal to 45 kg COD / m 3 .day, depending on the effluent to treat, while effectively removing more than 80% of the pollution contained in the effluent.
- the fluidization is temporary, the supports reorganizing in a fixed bed between each fluidization. It is also possible to keep the supports in suspension during the whole load step. The reactor then operates in a fluidized bed during this step.
- the accumulation of biomass is not detrimental to the operation of the reactor and, on the contrary, will make it possible to further increase the quantity of microorganisms in the reactor, which makes it possible to further increase the load applied in stationary operation. It is therefore no longer necessary to carry out frequent fluidizations.
- the reactor is maintained in fixed bed to promote the accumulation of biomass, in the form of biofilm and its accumulation in interstitial form and inside the supports.
- the major benefit of moving to fixed bed at the end of the start-up phase is to optimize energy costs by stopping the fluidization pump, as well as reducing the time required for reactor monitoring.
- the fixed-bed operation makes it possible to ensure filtration of the effluent and good retention of the solid particles in the reactor thanks to the filtering effect of the supports.
- the purification process according to the invention can be broken down into two main phases, namely:
- a first ramp-up phase between t0 and t + 1month, for example, during which the biomass is fixed on supports in the form of biofilm and the leaching of free biomass and interstitial biomass.
- the TSH is weak, and the COD gradually increased.
- a second stationary operating phase between t + 1 month and t °°, during which the reactor operates in a fixed bed, with a very spaced unclogging of the supports to evacuate excess biomass. During this second phase, retention is promoted by accumulation of biomass in the interstices of the supports.
- a reactor having a cylindrical PVC tank is used.
- the internal diameter of the tank is about 190 mm for a height of 1150 mm.
- height means the largest dimension of the vessel, parallel to the longitudinal axis of said vessel.
- This reactor has a useful volume of about 30 liters.
- the reactor is equipped with heating means making it possible to maintain the inside of the tank at a temperature of approximately 35 ° C.
- a feed pipe makes it possible to bring the effluent to be treated inside the tank, at the lower part of said tank.
- An evacuation pipe located in the upper part of the tank, makes it possible to evacuate the treated effluent.
- An overflow system makes it possible to maintain the liquid level at a height of 1000 mm in the tank.
- the reactor vessel contains polyethylene supports of generally cylindrical tubular shape.
- the supports fill about 60% of the volume of the tank. These supports have a density substantially equal to 0.93 and a specific surface area of 320 m 2 / m 3 .
- specific surface we mean the surface on which microorganisms are likely to cling to form a biofilm.
- the supports used have a large size compared to the supports usually used in moving bed, and a relatively small size compared to the supports usually used in fixed bed. More precisely, the supports used have dimensions of approximately 30 to 35 mm in height and approximately 29 mm in diameter.
- the reactor In order to be able to fluidize on demand the supports organized in fixed bed in the reactor, the reactor is equipped with an internal pump, fixed to the bottom of the tank so as to be immersed in the liquid contained in the tank.
- the internal pump constitutes the means of fluidization, that is to say unclogging, of the reactor.
- the flow rate of the pump is about 480 L / h.
- the effluent to be treated is distillery vinasse whose total COD is between 10 and 24 g / L with a soluble COD of between 10 and 19 g / L.
- the initial pH of the effluent is between 4 and 5.5.
- initial pH means the pH of the effluent at the time of being introduced into the reactor vessel. Before the depollution treatment in the reactor, the pH is brought to a neutral pH, that is to say about 7.
- the anaerobic inoculum used is from another anaerobic reactor that has been used to process distillery vinasse and has been concentrated by decantation.
- inoculum is meant groups of bacteria used to seed the reactor vessel.
- the amount of biomass on the supports is determined by measuring the dry weight of the supports previously heated at 100 ° C. for 24 hours. COD is measured conventionally by a colorimetric method (Jirka, 1975).
- Observations of reactor operation in a first step, in order to initialize the effluent treatment process, the reactor is activated so that the time during which the effluent to be treated remains in the reactor, that is to say the time TRH hydraulic retention, either high, and the applied volume load (OLR), that is to say the amount of pollution introduced into the reactor, per m 3 of reactor and per day, is low. Then the TRH was gradually decreased while IOLR was increased, increasing the volume of distillery vinasse introduced into the reactor.
- TRH hydraulic retention either high
- OLR applied volume load
- the reactor was used for 180 days. For the reactor to be considered efficient, it is estimated that the
- TRH must be as small as possible and IOLR as large as possible.
- FIG. 5 shows a graph showing the evolution of TRH and OLR over time in the reactor used.
- the OLR is low and remains below 5.6 g COD / L.day. HRT decreases rapidly from 35 days on day 1 to 5 days on day 81.
- the HRT increases slightly.
- the average value of the TRH is 7.7 days, due to insufficient availability of distillery vinasse.
- the OLR has a slight drop at the same time and is between 1.6 and 2.6 g COD / L. day.
- the HRT decreases rapidly to reach a minimum residence time of 0.7 days.
- the OLR increases very rapidly to reach values of up to 36 g COD / L.day.
- a fixed bed anaerobic reactor, containing an ordered carrier such as Cloisonyl has a much lower OLR, not exceeding 14 g COD / L.day.
- the first operating period is the reactor start-up phase and low charges are applied to avoid organic overload and allow the biomass to accumulate in the reactor.
- the purification efficiency is greater than 85%.
- the residence time is around 0.7 days and the applied load 30 g COD / L.day to eliminate more than 85% of the pollution of the effluent.
- Soluble COD at the outlet of the reactor being less than 5.5 g / L.
- the first sample is taken after 66 days of operation of the reactor, that is to say during the first period of operation.
- the average amount of biomass is 2.5 g per support.
- the second sample is taken after 156 days of operation of the reactor, that is to say during the second period of operation.
- the average amount of biomass is then 3.2 g per support.
- the biomass thus increased by 30% between day 66 and day 156.
- the third sample was taken after 180 days, that is to say at the end of the third period of operation.
- the average amount of biomass is 4.5 g per support.
- the total concentration of biomass fixed on the supports in the reactor is about 57 g / l of reactor. The biomass thus increases satisfactorily in the reactor.
- the concentration of microorganisms is 5 to 6 times higher with a specific activity maintained.
- Specific activity refers to the amount of COD that can be removed per kilogram of biomass.
- Reactor Performance The charge applied in the purification process according to the invention is greater than 30 g COD / L, while effectively eliminating more than 80% of the pollution contained in the effluent.
- the activity conventionally measured in a fixed-bed anaerobic reactor without any possible declogging is about 15 g COD / L.day.
- the performance of the reactor used in the invention is directly related to the ability of the microorganisms to attach to the supports and the absence of turbulence within said reactor. Leaving the reactor clogged allows the biomass to grow optimally. Unclogging, which takes place on demand, for example only once the user believes that the clogging can be detrimental, allows to increase the operating time of the reactor and maintain its performance throughout the use.
- each of the three supports R1, R2 and R3 is in accordance with the support 3 as represented in FIG. 4A.
- the supports R1, R2, R3 may be covered with biofilms fixed to said supports, but may also accumulate biomass in the orifices and interstices 17 formed between the fins 11 and the center 12 of said supports.
- the method according to the invention therefore allows a strong reduction in the size of the equipment.
- the reactor mainly allows retention by accumulation of the biomass, in addition to the conventional formation of a biofilm .
- retention of the biomass is meant its accumulation in the interstices of the supports and / or between the supports.
- the formation of biofilm leads to a reduction of the specific surface area and the activity of the biomass because of the recovery of the supports by successive layers of biofilm.
- the declogging system makes it possible to evacuate the excess biomass accumulating in the layer of supports.
- the effect of "biomass retention" by filtration is related to size, shape, hydrodynamics supports and fixed bed use of the reactor. This is therefore different from the so-called conventional biofilters which allow the retention by a stack of supports and not by the supports themselves.
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Abstract
Description
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Priority Applications (5)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
CA 2606062 CA2606062A1 (fr) | 2005-04-27 | 2006-04-27 | Procede d'epuration d'effluent en reacteur anaerobie |
MD20070287A MD4155B1 (ro) | 2005-04-27 | 2006-04-27 | Procedeu de epurare a apelor reziduale într-un reactor anaerob |
EP06743849A EP1874695A2 (fr) | 2005-04-27 | 2006-04-27 | Procédé d'épuration d'effluent en réacteur anaérobie |
US11/919,481 US7670489B2 (en) | 2005-04-27 | 2006-04-27 | Method for purifying effluent in an anaerobic reactor |
NO20076095A NO20076095L (no) | 2005-04-27 | 2007-11-26 | Fremgangsmate for rensing av et avlop i en anaerob reaktor |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0551092A FR2885126B1 (fr) | 2005-04-27 | 2005-04-27 | Procede d'epuration d'effluent en reacteur anaerobie, et utilisation d'un reacteur biologique pour le traitement d'effluent |
FR0551092 | 2005-04-27 |
Publications (2)
Publication Number | Publication Date |
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WO2006114552A2 true WO2006114552A2 (fr) | 2006-11-02 |
WO2006114552A3 WO2006114552A3 (fr) | 2007-04-12 |
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Application Number | Title | Priority Date | Filing Date |
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PCT/FR2006/050392 WO2006114552A2 (fr) | 2005-04-27 | 2006-04-27 | Procédé d'épuration d'effluent en réacteur anaérobie |
Country Status (8)
Country | Link |
---|---|
US (1) | US7670489B2 (fr) |
EP (1) | EP1874695A2 (fr) |
CA (1) | CA2606062A1 (fr) |
FR (1) | FR2885126B1 (fr) |
MD (1) | MD4155B1 (fr) |
NO (1) | NO20076095L (fr) |
UA (1) | UA89402C2 (fr) |
WO (1) | WO2006114552A2 (fr) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
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EP2438019A4 (fr) * | 2009-06-03 | 2015-06-03 | Biowater Technology AS | Procédé et réacteur pour l'épuration biologique des eaux usées |
FR3025511A1 (fr) * | 2014-09-05 | 2016-03-11 | Eau Et Ind | Procede d'intensification du traitement des eaux usees par lagunage assurant l'elimination de l'azote et du phosphore |
Families Citing this family (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
WO2009107128A2 (fr) * | 2008-02-25 | 2009-09-03 | Aqwise - Wise Water Technologies Ltd. | Supports de biomasse, procédé et appareil pour leur fabrication, systèmes et procédés de traitement de fluides les utilisant |
WO2010026564A1 (fr) * | 2008-09-03 | 2010-03-11 | Aqwise - Wise Water Technologies Ltd. | Traitement et clarification biologiques intégrés des eaux usées |
IT1393126B1 (it) * | 2009-03-05 | 2012-04-11 | Eni Spa | Processo per la purificazione di una corrente acquosa proveniente dalla reazione di fischer-tropsch |
US8758613B2 (en) * | 2009-10-16 | 2014-06-24 | Aqwise-Wise Water Technologies Ltd | Dynamic anaerobic aerobic (DANA) reactor |
CN102910780B (zh) * | 2012-07-06 | 2013-10-16 | 广州市环境保护工程设计院有限公司 | 一种用于处理高含盐量难降解废水的装置及处理方法 |
JP5985425B2 (ja) * | 2013-03-25 | 2016-09-06 | 株式会社クボタ | 汚水処理装置の稼動方法 |
US9108868B1 (en) * | 2013-10-31 | 2015-08-18 | Premier Magnesia, Llc | Treatment of potable water |
MD885Z (ro) * | 2014-08-11 | 2015-09-30 | Институт Прикладной Физики Академии Наук Молдовы | Reactor şi procedeu de obţinere a hidrogenului |
EP3429719B1 (fr) | 2016-03-18 | 2021-10-13 | Parkson Corporation | Procédé amélioré pour nettoyer des supports de système de filtration |
US10913667B2 (en) * | 2017-12-08 | 2021-02-09 | Westech Engineering, Inc. | Multi-media clarification systems and methods |
CN109437395B (zh) * | 2018-11-28 | 2023-09-12 | 北京工业大学 | 一种实现城市生活污水厌氧产甲烷的装置和运行方法 |
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US5147547A (en) * | 1990-12-03 | 1992-09-15 | Degremont S.A. | Oxidation and biological reduction reactor, biofiltration method and washing methods used in this reactor |
DE19929568A1 (de) * | 1999-03-24 | 2000-09-28 | Volker Harbs | Verfahren zur Wasseraufbereitung und Abwasserreinigung unter Verwendung eines Schwebefilterbettes |
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US4043936A (en) * | 1976-02-24 | 1977-08-23 | The United States Of America As Represented By United States Energy Research And Development Administration | Biological denitrification of high concentration nitrate waste |
US4322196A (en) * | 1980-04-24 | 1982-03-30 | Hinshaw Carl F | Soup retort |
NZ226453A (en) * | 1987-10-08 | 1990-04-26 | Gist Brocades Nv | Anaerobic purification of waste water using granular sludge in fluidised bed process |
US5006249A (en) * | 1988-12-29 | 1991-04-09 | Exxon Research And Engineering Company | Anaerobic waste water treating process |
US5126042A (en) * | 1991-10-31 | 1992-06-30 | Malone Ronald F | Floating media biofilter |
US5750041A (en) * | 1994-08-15 | 1998-05-12 | Hirane; Ken | Method for backwashing water processing systems |
US6447675B1 (en) * | 2000-08-29 | 2002-09-10 | Ron James | Fish pond filter system |
US6709591B1 (en) * | 2001-07-02 | 2004-03-23 | Iowa State University Research Foundation, Inc. | Static granular bed reactor |
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2005
- 2005-04-27 FR FR0551092A patent/FR2885126B1/fr not_active Expired - Fee Related
-
2006
- 2006-04-27 WO PCT/FR2006/050392 patent/WO2006114552A2/fr active Application Filing
- 2006-04-27 CA CA 2606062 patent/CA2606062A1/fr not_active Abandoned
- 2006-04-27 UA UAA200711847A patent/UA89402C2/ru unknown
- 2006-04-27 EP EP06743849A patent/EP1874695A2/fr not_active Withdrawn
- 2006-04-27 MD MD20070287A patent/MD4155B1/ro not_active IP Right Cessation
- 2006-04-27 US US11/919,481 patent/US7670489B2/en not_active Expired - Fee Related
-
2007
- 2007-11-26 NO NO20076095A patent/NO20076095L/no not_active Application Discontinuation
Patent Citations (3)
Publication number | Priority date | Publication date | Assignee | Title |
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US4322296A (en) * | 1980-08-12 | 1982-03-30 | Kansas State Univ. Research Foundation | Method for wastewater treatment in fluidized bed biological reactors |
US5147547A (en) * | 1990-12-03 | 1992-09-15 | Degremont S.A. | Oxidation and biological reduction reactor, biofiltration method and washing methods used in this reactor |
DE19929568A1 (de) * | 1999-03-24 | 2000-09-28 | Volker Harbs | Verfahren zur Wasseraufbereitung und Abwasserreinigung unter Verwendung eines Schwebefilterbettes |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2438019A4 (fr) * | 2009-06-03 | 2015-06-03 | Biowater Technology AS | Procédé et réacteur pour l'épuration biologique des eaux usées |
US9758402B2 (en) | 2009-06-03 | 2017-09-12 | Biowater Technology AS | Method and reactor for biological purification of waste water |
FR3025511A1 (fr) * | 2014-09-05 | 2016-03-11 | Eau Et Ind | Procede d'intensification du traitement des eaux usees par lagunage assurant l'elimination de l'azote et du phosphore |
Also Published As
Publication number | Publication date |
---|---|
US20090078648A1 (en) | 2009-03-26 |
FR2885126A1 (fr) | 2006-11-03 |
WO2006114552A3 (fr) | 2007-04-12 |
CA2606062A1 (fr) | 2006-11-02 |
MD20070287A (en) | 2008-03-31 |
MD4155B1 (ro) | 2012-03-31 |
EP1874695A2 (fr) | 2008-01-09 |
NO20076095L (no) | 2008-01-25 |
FR2885126B1 (fr) | 2007-08-10 |
US7670489B2 (en) | 2010-03-02 |
UA89402C2 (ru) | 2010-01-25 |
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