WO2011055092A1 - Procede de traitement anaerobie d'une eau usee et dispositif associe - Google Patents
Procede de traitement anaerobie d'une eau usee et dispositif associe Download PDFInfo
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- WO2011055092A1 WO2011055092A1 PCT/FR2010/052381 FR2010052381W WO2011055092A1 WO 2011055092 A1 WO2011055092 A1 WO 2011055092A1 FR 2010052381 W FR2010052381 W FR 2010052381W WO 2011055092 A1 WO2011055092 A1 WO 2011055092A1
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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
- C02F3/006—Regulation methods for biological treatment
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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
- C02F3/005—Combined electrochemical biological 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
- C02F3/28—Anaerobic digestion processes
- C02F3/2853—Anaerobic digestion processes using anaerobic membrane bioreactors
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/46—Treatment of water, waste water, or sewage by electrochemical methods
- C02F1/469—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis
- C02F1/4693—Treatment of water, waste water, or sewage by electrochemical methods by electrochemical separation, e.g. by electro-osmosis, electrodialysis, electrophoresis electrodialysis
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F1/00—Treatment of water, waste water, or sewage
- C02F1/66—Treatment of water, waste water, or sewage by neutralisation; pH adjustment
-
- 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
- C02F2209/04—Oxidation reduction potential [ORP]
-
- 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
- C02F2209/06—Controlling or monitoring parameters in water treatment pH
-
- 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
- C02F2209/12—Volatile Fatty Acids (VFAs)
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/10—Temperature conditions for biological treatment
- C02F2301/103—Psychrophilic treatment
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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
- C02F2301/00—General aspects of water treatment
- C02F2301/10—Temperature conditions for biological treatment
- C02F2301/106—Thermophilic treatment
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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
- 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 method for the anaerobic treatment of waste water and an associated device.
- the invention is in the field of biological treatment systems of urban and industrial wastewater carrying a high concentration of organic matter (more than 1 kg / m 3 , or even more than 3 kg / m 3 ) and characterized by a production at least one by-product, for example volatile fatty acids (VFA).
- a threshold for qualifying such a production of high production of AGV is for example 200 mg per liter of treated water.
- the first is the stopping of the diet of the gross influent or its dilution; and the second is the addition of chemicals (eg calcium salts or soda) for the precipitation of by-products.
- chemicals eg calcium salts or soda
- reaction products are not recovered whereas they could be recovered if they were extracted from the reaction mixture.
- US 3 71 1 392 discloses a method of using organic waste involving a fermentation tank, a precipitation tank and an electrodialysis apparatus. The goal is the preparation of food products.
- EP 1 236 688 discloses a biological waste water treatment plant equipped with anaerobic digesters.
- a reactor has an inclined base for gravity removal of heavy metals and non-biodegradable products from acidogenic bacteria.
- US 6391598 discloses a method for preparing metal salts of fatty acids from an anaerobic digestive tract of ruminant.
- Kim et al., Desalination, 172, 2005, 1 19 presents results of experimental work relating to the filtration performance of a system consisting of a 35 ° C fermentor coupled to a ceramic-monolithic microfiltration membrane. tubular from 0.5 ⁇ to 5 ⁇ pore diameter - for the extraction of organic compounds dissolved in a sludge. The pH is adjusted with sodium hydroxide and hydrochloric acid.
- Camargo et al. (IX Latin American Symposium on Anaerobic Digestion, October 2008) presents results of experimental work on the association of an electrodialysis unit with an anaerobic submicron submersible reactor with a pore size of 10 ⁇ .
- electrodialyser is used to adapt the microorganisms to the AGV in the reactor by controlled recirculation of AGV in the reactor, which can lead to an increase in the organic load.
- the technical problem addressed is to reduce the presence of byproducts having an inhibitory or even a blocking effect for the formation of biogas in the reaction mixture without stopping the supply of organic matter or introducing chemical reagents.
- the objective is to improve the performance of methane formation by extracting toxic products (or inhibitors), including AGV, ammonia or h limiting the formation of biogas.
- an anaerobic treatment method for waste water is proposed in a biological reactor involving at least one stabilized-regime bacterial species comprising the following steps:
- the various steps of the process can be advantageously regular, even semi-continuous or continuous.
- the relative proportions of the flow rates of the first and second sub-fractions are chosen as a function of the concentration of reaction products (AGV or other inhibitory product) in the reaction mixture of the biological reactor and the solubilization capacity of a dilution solution used in the reaction mixture. the separation process. In the case of one embodiment, 1 volume of dilution solution and 9 volumes of the reaction mixture are used.
- the production of biogas in particular methane, is a function of the transformed organic load, and thus of the Total Organic Carbon (TOC) consumed.
- TOC Total Organic Carbon
- the efficiency of the process is measured by one or other of these two parameters (biogas production or TOC consumption).
- said zone connected to the reactor comprises an inner zone of the reactor and a wastewater supply pipe to be treated, an outlet pipe and optionally a recirculation pipe resulting from the liquid / solid separation and / or outlet the effluent outlet.
- the measurement points are, depending on the embodiments, before the reactor, in the reactor, on a recirculation pipe, or on an outlet pipe. Extraction of a fraction of the reactor contents is done either at the reactor itself, at the outlet line, at the recirculation line, or at the feed line. either at the level of the feed tank, before entering the biological reactor, especially if there is a large production of reaction product at this level.
- the reactor is fixed bed, which allows to contain the amount of free biomass. It can also be fluidized bed or free biomass.
- the biological reactor comprises, in alternative embodiments, in place of the fixed bed, a granular bed, a bed in suspension or a mixture of biomass fixed on inert supports and activated sludge. According to an advantageous characteristic, between the extraction and the separation, a filtration step is carried out with a pore membrane smaller than 5 ⁇ .
- liquid / solid separator such as hydrocylone, sand filter, decanters, sieves, centrifuge.
- said filtration step is carried out with a pore ceramic membrane 1, 2 ⁇ in diameter.
- the reactor is a mesophilic or thermophilic reactor, said reaction product being a set of volatile fatty acids, and said zone being a liquid phase zone.
- the temperature range of the reactor is 25 to 40 ° C, or 40 to 65 ° C, for the mesophilic and thermophilic microorganisms respectively.
- microorganisms present in an alternative embodiment are psychrophilic, and are active in the temperature range of 0 to 25 ° C.
- the amount and type of organic matter in the wastewater to be treated, the hydraulic retention time and the type of microorganism determine the level of production and accumulation of VFA.
- the predefined threshold is at least 200 mg / L of AGV. In one embodiment, a decrease in CH 4 production is observed from 200 mg / L of AGV.
- the extraction is triggered as a function of the energy costs of the start of the extraction process with regard to the energy savings due to the improvement of the CH production process.
- the trigger threshold value is re-evaluated upwards.
- This value is an average value which is advantageous from the energy gain point of view.
- the measuring system is clocked by a clock that measures the AGV concentration at a regular interval in a reactor zone.
- the extraction device is not implemented. road.
- the senor during its measurement operation performed at regular intervals, measures a value of 1.2 g / l, a value greater than 1 g / l, and triggers on this basis the start of the extraction process.
- the threshold value of AGV is further determined by the degree of adaptation of microorganisms to AGVs and the cost / benefit ratio of the extraction process.
- the separation is carried out using an electrodialyzer.
- the electrodialyzer comprises a membrane CMX (cation exchange membrane) and / or AMX (anion exchange membrane).
- CMX cation exchange membrane
- AMX anion exchange membrane
- an electrodialyser consisting of cells comprising both an anionic membrane and a cationic membrane is used.
- the pH of the reactor is maintained between 6.5 and 7.5
- This pH range is optimal to allow the development of methanogenic microorganisms.
- the water is an effluent from the food industry or an urban effluent.
- a controlled recirculation line is used for doping the reactor with the second sub-fraction.
- the invention also proposes a device for anaerobic treatment of wastewater in a biological reactor involving at least one stabilized-state bacterial species comprising means for:
- the device according to the invention is provided with means or functions corresponding to the characteristics mentioned above with regard to the method according to the invention.
- the invention will now be described in detail with reference to the accompanying figures.
- Figure 1 shows a general diagram of the invention.
- Figure 2 shows a diagram of a particular embodiment of the invention.
- FIG. 3 to 6 show other variants of the invention.
- Figure 7 shows a second embodiment of the invention.
- FIGS. 8 to 10 show parameters measured during a scenario of implementation of a method according to the invention.
- a wastewater treatment reactor 100 is supplied upstream, for example, by a feed tank (or buffer tank) 120, via a supply line 1 10.
- the wastewater here is a waste water having an organic matter concentration of between 20 and 30 kg / m 3 . In this order of magnitude of organic charge, it is in the case of industrial water. Waste urban water, to which the invention can also be applied, generally contains a concentration of organic matter at around 1 kg / m 3 .
- the reactor has an effluent outlet 130 and a methane outlet 135. It is a thermophilic biological reactor at 55 ° C., for example a fixed bed with plastic material as support, of ascending flow.
- the reactor has an automatic pH control device that maintains the pH in a range of 6.5 to 7.5.
- This device operates in the following way: the pH meter is placed in the reactor, then the pH meter is connected to a computer which contains a decision algorithm for controlling, by means of feed pumps, the supply of acidic solution such as hydrochloric acid HCl, phosphoric acid H 2 PO 4 or sulfuric acid H 2 SO 4, or basic solution, preferably sodium hydroxide NaOH, depending on the pH in the reactor.
- acidic solution such as hydrochloric acid HCl, phosphoric acid H 2 PO 4 or sulfuric acid H 2 SO 4
- basic solution preferably sodium hydroxide NaOH
- the redox potential measured for example by means of a redox-meter, in the reactor must preferably be kept below a threshold value of -200mV. Maintaining the redox potential below said threshold value, well known to those skilled in the art, allows optimal development of methanogenic bacteria.
- a measurement of the concentration of volatile fatty acids (VFA) is carried out in the reactor at a measuring point 150, using an on-line analyzer. This monitors the position of the AGV concentration, measured in acetic acid equivalent, relative to the threshold value of 1 g / L.
- an extraction line 160 continuously extracts a fraction of the volume of the reactor 100 and brings it to a solid / liquid separator 200 which is here a microfiltration system with ceramic membranes of 1. 2 ⁇ of pore diameter (depending on the variants, it is possible to perform microfiltration or ultrafiltration). It is specified that this separator is optional.
- Various means are used to effect the separation between liquid and solid, depending on the embodiments, such as hydrocylone, centrifuge, sand filter, decanters, sieves.
- the extraction rate in one embodiment is less than or equal to 10 times the feed rate of the biological reactor.
- a line 210 returns solids separated by the separator to the reactor 100.
- Line 220 feeds the liquid filtrate to an electrodialyser 300, which produces two sub-fractions, one of which is depleted of AGV, and the other enriched.
- the proportions are functions of the concentration of AGV (or other inhibitor product) in the reaction mixture of the biological reactor and the solubilization capacity of the dilution solution used. In the case of the tests carried out, it took 1 volume of dilution solution and 9 volumes of the reaction mixture.
- the depleted fraction is fed to the reactor via line 310 and the enriched fraction is removed from the system via line 320 to be supported by processes that are not within the scope of this disclosure.
- the concentration of organic material applied was between 2 and 100 kg / m3 day.
- the hydraulic retention time was between 18 and 96 hours.
- the hydraulic retention time is the average residence time of the effluent in the reactor.
- FIG. 8 shows the impact of VFA accumulation on biogas production (methane). It can be seen that the higher the accumulation of VFAs, the lower the biogas production.
- the biogas production and the AGV concentration are represented on the ordinate (right axis and left axis respectively), the abscissae defining the operating time in days.
- This figure shows the impact of AGVs on biogas production.
- AGV concentrations lower than 400 mg.L “1 and close to 200 mg.L " 1
- the maximum biogas production is greater than 16 Lj "1.
- biogas production is reduced by more than 50% and more than 75% for AGV concentrations above 1000 mg.L " 1 .
- the 1 .2 ⁇ m filtration system was started when the AGV concentration reached a value in the reaction mixture of 1.2 g / L.
- the AGV concentration is reduced by 50% after a time of the order of 2 minutes as illustrated in FIG. 9, which shows the variations of the concentration of AGV in the effluent as a function of time during the implementation scenario. process of the invention, with a voltage of 12.4 V.
- This figure shows the concentration of AGV on the left ordinate axis in mg / L, and the extraction of AGV percentage on the axis ordinates on the right, the abscissae representing the duration of the test in minutes.
- the initial concentration is of the order of 1200 mg / L. It decreases in two phases, from 0 to 2 minutes to a value of 500 mg / L, then from 5 to 9 minutes, up to a value of 250 mg / L.
- Figure 10 shows finally that all the AGV are extracted which is manifested by the lifting of the inhibition of the production of biogas.
- This figure shows the initial concentration and the final concentration (y-axis on the left, in mg / L), and the extraction yield (right-y axis, in percentage), for acetic, propionic acids. isobutyric, butyric, isovaleric, valeric, hexanoic (absent) and heptanoic (absent), as well as for the entire family of volatile fatty acids. Yields are always above 65%, and the total yield is around 90%.
- the main acids concerned are acetic acid and propionic acid, their initial concentrations being of the order of 1200 to 1900 mg / L, with an associated extraction yield of the order of 85%.
- the line 1100 allows a controlled recirculation of a concentrated solution of volatile fatty acids from the electrodialyzer 300 (concentrated subfraction resulting from the separation), thus inducing doping, preferably at low flow.
- the extracted products are thus used for the regulation of the reactor charge, and the establishment of favorable conditions for the adaptation over time of the biomass to the compounds which it is desired to promote and which were inhibitory. for non adapted biomass.
- an on-line analyzer placed at the measuring point 151 monitors the concentration of AGV at the effluent outlet 130.
- the operation of the system is similar to that described with reference to FIG. trigger is suitable.
- an in-line analyzer at measurement point 152 monitors the concentration of AGV or other by-products in supply line 1 10, or in feed tank 120, which is useful if the material to be treated contains inhibitory or toxic compounds.
- the operation of the system is similar to that described with reference to FIG. 1, but the triggering threshold is adapted.
- an in-line analyzer at measurement point 153 monitors the AGV concentration in the solids recirculation conduit 210.
- the operation of the system is similar to that described in connection with Fig. 1, but the trigger threshold is suitable.
- an in-line analyzer at measurement point 154 monitors the AGV concentration in the recirculation line of depleted fraction 310.
- the on-line analyzer 154 allows the verification of the AGV concentration in the fraction depleted of AGV and to ensure that this concentration is below the trigger threshold of the electrodialyzer.
- an on-line analyzer 155 measures the concentration of AGV in the reactor and controls the operation of the electrodialyzer 300.
- the analyzer 155 regulates the operation of the pump (not shown), which conveys the liquid from the reactor 100 into the electrodialyser 300, depending on the concentration of AGV.
- the result of this double measurement in line makes it possible to adjust the operating time of the electro-dialyzer 300.
- This configuration is particularly suitable for the case of effluents from the food industry including sweets whose amount of easily biodegradable carbon is important.
- the operation of the system is similar to that described with reference to FIG. 1, but the triggering threshold is adapted.
- the biomass may be free (that is to say so-called flocculant sludge or so-called granular sludge) or fixed biomass (that is to say on supports of one type or another on which the biomass is fixed).
- the supports on which the biomass is fixed can be contained between two grids or retained by a grid acting as a ceiling or as a floor - depending on the direction of the fluid, and in this case, the supports, on which the biomass is fixed, are arranged in a fixed bed.
- the supports on which the biomass is fixed may be in suspension, presented in the form of a fluidized bed.
- the extracted by-product is ammonia (NH 3 ), ammonium ions (NH + ), or dihydrogen (H 2 ), and the phase in which the extraction is made is the liquid or gaseous phase.
- a threshold for dihydrogen is 5.8 Pa, the extraction technique used being then based on a membrane switch (also valid for ammonia).
- This variant constitutes an embodiment shown in FIG. 7, in which a biological reactor 5100 is observed with an effluent feed 5120, an effluent outlet 5130, a gas mixture extraction line 5160, a measurement in line at point 5150 of the concentration of methane, dihydrogen or ammonia (in the gaseous atmosphere above the liquid phase), for example, a 5200 pretreatment system (optional) and a 5300 by-product extraction reactor, with an extraction pipe for recovery at mark 5320, a pipe for recirculation 5310 of the fraction depleted by by-product and a recirculation pipe controlled 6100 of a solution concentrated by-product, the pipes 5310 and 6100 allowing recirculation to the reactor.
- a biological reactor 5100 is observed with an effluent feed 5120, an effluent outlet 5130, a gas mixture extraction line 5160, a measurement in line at point 5150 of the concentration of methane, dihydrogen or ammonia (in the gaseous atmosphere above the liquid phase), for example
Abstract
Description
Claims
Priority Applications (4)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2010316835A AU2010316835B2 (en) | 2009-11-06 | 2010-11-04 | Method for anaerobic treatment of wastewater and associated device |
EP10795420A EP2496529A1 (fr) | 2009-11-06 | 2010-11-04 | Procede de traitement anaerobie d'une eau usee et dispositif associe |
US13/508,142 US20120219984A1 (en) | 2009-11-06 | 2010-11-04 | Method for the anaerobic treatment of a wastewater and associated device |
CA 2780185 CA2780185A1 (fr) | 2009-11-06 | 2010-11-04 | Procede de traitement anaerobie d'une eau usee et dispositif associe |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0957887A FR2952369B1 (fr) | 2009-11-06 | 2009-11-06 | Procede de traitement anaerobie d'une eau usee et dispositif associe |
FR0957887 | 2009-11-06 |
Publications (1)
Publication Number | Publication Date |
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WO2011055092A1 true WO2011055092A1 (fr) | 2011-05-12 |
Family
ID=42269407
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
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PCT/FR2010/052381 WO2011055092A1 (fr) | 2009-11-06 | 2010-11-04 | Procede de traitement anaerobie d'une eau usee et dispositif associe |
Country Status (6)
Country | Link |
---|---|
US (1) | US20120219984A1 (fr) |
EP (1) | EP2496529A1 (fr) |
AU (1) | AU2010316835B2 (fr) |
CA (1) | CA2780185A1 (fr) |
FR (1) | FR2952369B1 (fr) |
WO (1) | WO2011055092A1 (fr) |
Cited By (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
LU91846B1 (en) * | 2011-07-22 | 2013-01-23 | Ct De Rech Public Gabriel Lippmann | Process for controlling and monitoring the production of biogas |
WO2019081252A1 (fr) | 2017-10-26 | 2019-05-02 | Veolia Environnement | Procédé de fermentation acidogène pour la production d'acides organiques de 2 à au moins 5 atomes de carbone et installation correspondante |
Families Citing this family (4)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
EP2706044A1 (fr) * | 2012-09-07 | 2014-03-12 | Siemens Aktiengesellschaft | Traitement des eaux usées, en particulier des eaux de mines contenant des métaux lourds et/ou des sulfates |
LU92192B1 (fr) * | 2013-05-13 | 2014-11-14 | Emmanuel Trouve | Procédé et dispositif de traitement d'une biomassemélangée à de l'eau pour produire de l'eau potabl e, du biogaz et des matières sèches combustibles |
US11920248B2 (en) | 2018-12-18 | 2024-03-05 | Prometheus Fuels, Inc | Methods and systems for fuel production |
KR20230148199A (ko) * | 2021-02-19 | 2023-10-24 | 프로메테우스 퓨얼즈, 인크. | 이산화탄소의 통합된 직접 공기 포집 및 전기화학적 환원 |
Citations (11)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3711392A (en) | 1971-02-16 | 1973-01-16 | J Metzger | Method for the utilization of organic waste material |
US4781836A (en) * | 1986-05-16 | 1988-11-01 | Michigan Biotechnology Institute | Method for biomethanation |
EP0422876A1 (fr) * | 1989-10-09 | 1991-04-17 | Shimizu Construction Co., Ltd. | Procédé et appareil pour la commande de traitement d'eau usée par fermentation anaérobic |
EP0970922A2 (fr) * | 1998-07-06 | 2000-01-12 | Kubota Corporation | Procédé de fermentation methanique de déchets organiques |
US6391598B1 (en) | 1999-03-29 | 2002-05-21 | Board Of Regents Of The University Of Nebraska | Preparation of fatty acid metal salts and enzymes from ruminal fluid |
EP1236688A1 (fr) | 1999-11-12 | 2002-09-04 | Insertam S.L. | Centrale d'epuration biologique d'eaux residuelles equipee de digesteurs anaerobies et procede d'epuration |
US20020192809A1 (en) * | 2001-05-31 | 2002-12-19 | Biothane Corporation | Anaerobic digestion apparatus methods for anaerobic digestion and for minimizing the use of inhibitory polymers in digestion |
WO2005035693A2 (fr) | 2003-10-02 | 2005-04-21 | Mississippi State University | Production de biodiesel et d'autres produits chimiques interessants a partir de boues d'installations de traitement des eaux usees |
WO2009153437A2 (fr) * | 2008-05-26 | 2009-12-23 | Otv Sa | Procédé de traitement biologique d'un effluent et installation associée |
EP2135938A1 (fr) * | 2008-06-20 | 2009-12-23 | Sergio Trabattoni | Procédé et installation de fermentation anaérobique |
WO2010046913A2 (fr) * | 2008-10-06 | 2010-04-29 | Kirloskar Integrated Technologies Ltd. | Procédé de filtration sélective pour produire du biogaz |
Family Cites Families (5)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR2447350A1 (fr) * | 1979-01-24 | 1980-08-22 | France Syndicat Fab Sucre | Fermenteur decanteur anaerobie pour l'epuration d'eaux residuaires de sucrerie avec recuperation de methane combustible |
US5514277A (en) * | 1993-04-12 | 1996-05-07 | Khudenko; Boris M. | Treatment of wastewater and sludges |
US20060000358A1 (en) * | 2004-06-29 | 2006-01-05 | Rajat Agrawal | Purification and delivery of high-pressure fluids in processing applications |
CA2605468C (fr) * | 2005-05-03 | 2016-04-12 | Anaerobe Systems | Production anaerobie d'hydrogene et d'autres produits chimiques |
CA2765767C (fr) * | 2009-06-16 | 2017-09-26 | Cambrian Innovation, Inc. | Systemes et dispositifs pour traiter et surveiller de l'eau, des eaux usees et autres matieres biodegradables |
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2009
- 2009-11-06 FR FR0957887A patent/FR2952369B1/fr active Active
-
2010
- 2010-11-04 US US13/508,142 patent/US20120219984A1/en not_active Abandoned
- 2010-11-04 WO PCT/FR2010/052381 patent/WO2011055092A1/fr active Application Filing
- 2010-11-04 CA CA 2780185 patent/CA2780185A1/fr not_active Abandoned
- 2010-11-04 EP EP10795420A patent/EP2496529A1/fr not_active Withdrawn
- 2010-11-04 AU AU2010316835A patent/AU2010316835B2/en not_active Ceased
Patent Citations (12)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
US3711392A (en) | 1971-02-16 | 1973-01-16 | J Metzger | Method for the utilization of organic waste material |
US4781836A (en) * | 1986-05-16 | 1988-11-01 | Michigan Biotechnology Institute | Method for biomethanation |
EP0422876A1 (fr) * | 1989-10-09 | 1991-04-17 | Shimizu Construction Co., Ltd. | Procédé et appareil pour la commande de traitement d'eau usée par fermentation anaérobic |
EP0970922A2 (fr) * | 1998-07-06 | 2000-01-12 | Kubota Corporation | Procédé de fermentation methanique de déchets organiques |
US6391598B1 (en) | 1999-03-29 | 2002-05-21 | Board Of Regents Of The University Of Nebraska | Preparation of fatty acid metal salts and enzymes from ruminal fluid |
EP1236688A1 (fr) | 1999-11-12 | 2002-09-04 | Insertam S.L. | Centrale d'epuration biologique d'eaux residuelles equipee de digesteurs anaerobies et procede d'epuration |
US20020192809A1 (en) * | 2001-05-31 | 2002-12-19 | Biothane Corporation | Anaerobic digestion apparatus methods for anaerobic digestion and for minimizing the use of inhibitory polymers in digestion |
WO2005035693A2 (fr) | 2003-10-02 | 2005-04-21 | Mississippi State University | Production de biodiesel et d'autres produits chimiques interessants a partir de boues d'installations de traitement des eaux usees |
US20050112735A1 (en) | 2003-10-02 | 2005-05-26 | Zappi Mark E. | Production of biodiesel and other valuable chemicals from wastewater treatment plant sludges |
WO2009153437A2 (fr) * | 2008-05-26 | 2009-12-23 | Otv Sa | Procédé de traitement biologique d'un effluent et installation associée |
EP2135938A1 (fr) * | 2008-06-20 | 2009-12-23 | Sergio Trabattoni | Procédé et installation de fermentation anaérobique |
WO2010046913A2 (fr) * | 2008-10-06 | 2010-04-29 | Kirloskar Integrated Technologies Ltd. | Procédé de filtration sélective pour produire du biogaz |
Non-Patent Citations (2)
Title |
---|
CAMARGO ET AL., IX SYMPOSIUM LATINO-AMÉRICAIN SUR LA DIGESTION ANAÉROBIE, October 2008 (2008-10-01) |
KIM ET AL., DESALINATION, vol. 172, 2005, pages 119 |
Cited By (3)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
LU91846B1 (en) * | 2011-07-22 | 2013-01-23 | Ct De Rech Public Gabriel Lippmann | Process for controlling and monitoring the production of biogas |
EP2548849A1 (fr) * | 2011-07-22 | 2013-01-23 | Centre de Recherche Public - Gabriel Lippmann | Procédé pour contrôler et surveiller la production de biogaz |
WO2019081252A1 (fr) | 2017-10-26 | 2019-05-02 | Veolia Environnement | Procédé de fermentation acidogène pour la production d'acides organiques de 2 à au moins 5 atomes de carbone et installation correspondante |
Also Published As
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FR2952369A1 (fr) | 2011-05-13 |
US20120219984A1 (en) | 2012-08-30 |
AU2010316835A1 (en) | 2012-06-21 |
CA2780185A1 (fr) | 2011-05-12 |
AU2010316835B2 (en) | 2015-09-10 |
FR2952369B1 (fr) | 2017-05-19 |
EP2496529A1 (fr) | 2012-09-12 |
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