WO2008132296A2 - Procede et installation de traitement d'eaux usees contenant des sulfures et de l'ammonium - Google Patents
Procede et installation de traitement d'eaux usees contenant des sulfures et de l'ammonium Download PDFInfo
- Publication number
- WO2008132296A2 WO2008132296A2 PCT/FR2008/000255 FR2008000255W WO2008132296A2 WO 2008132296 A2 WO2008132296 A2 WO 2008132296A2 FR 2008000255 W FR2008000255 W FR 2008000255W WO 2008132296 A2 WO2008132296 A2 WO 2008132296A2
- Authority
- WO
- WIPO (PCT)
- Prior art keywords
- anoxic
- treatment
- sulphides
- basin
- nitrates
- Prior art date
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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
- C02F3/34—Biological treatment of water, waste water, or sewage characterised by the microorganisms used
- C02F3/345—Biological treatment of water, waste water, or sewage characterised by the microorganisms used for biological oxidation or reduction of sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/006—Regulation methods for biological treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/30—Aerobic and anaerobic processes
- C02F3/302—Nitrification and denitrification treatment
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/101—Sulfur compounds
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2101/00—Nature of the contaminant
- C02F2101/10—Inorganic compounds
- C02F2101/16—Nitrogen compounds, e.g. ammonia
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/005—Processes using a programmable logic controller [PLC]
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/06—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
- C02F2209/08—Chemical Oxygen Demand [COD]; Biological Oxygen Demand [BOD]
-
- 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
- C02F2209/15—N03-N
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- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/20—Total organic carbon [TOC]
-
- 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
- C02F2209/26—H2S
-
- 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
- C02F2209/40—Liquid flow rate
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F2209/00—Controlling or monitoring parameters in water treatment
- C02F2209/44—Time
-
- C—CHEMISTRY; METALLURGY
- C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
- C02F3/00—Biological treatment of water, waste water, or sewage
- C02F3/02—Aerobic processes
- C02F3/12—Activated sludge processes
- C02F3/1236—Particular type of activated sludge installations
- C02F3/1263—Sequencing batch reactors [SBR]
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- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02W—CLIMATE CHANGE MITIGATION TECHNOLOGIES RELATED TO WASTEWATER TREATMENT OR WASTE MANAGEMENT
- Y02W10/00—Technologies for wastewater treatment
- Y02W10/10—Biological treatment of water, waste water, or sewage
Definitions
- the invention relates to a process for the treatment of sulphide and ammonium-laden wastewater, in particular waste water of urban or industrial origin or digestion returns, condensates, leachates.
- Wastewater contains in particular carbon, nitrogen and sulfur in various forms of compounds that can be chemically treated by various processes. All physico-chemical treatments consist in separating the compounds of these elements from one liquid phase to concentrate them in another phase. These include the processes of stripping (removal of gas in the water by means of a driving gas), reverse osmosis, distillation, chemical precipitation or catalytic oxidation, the costs of implementation and operating costs are high.
- the organic carbonaceous material is oxidized in aerated medium by microorganisms, mainly heterotrophic bacteria. These microorganisms use the organic carbonaceous, colloidal and dissolved material and converts it into gas or into biomass.
- nitrification and denitrification treatments are mainly distinguished, by which ammonium is oxidized in two stages under conditions aerated by autotrophic bacteria (first nitrite then nitrate), and finally reduced to gaseous nitrogen under anoxic conditions by heterotrophic bacteria.
- Sulphates are naturally present in wastewater, and sulfur is included in the intracellular protein composition of microorganisms. Sulfur can be oxidized or reduced depending on the environmental conditions and the populations of bacteria present. In an aerobic environment, sulphides are converted into sulphates by sulphooxidizing bacteria and in anaerobic medium, the sulphates are converted into sulphides by sulphate-reducing bacteria.
- the first reactor makes it possible to reduce sulphates to sulphides and to treat the carbon charge.
- the sulphides are oxidized to sulphates by reducing the nitrates from the recirculation of the aerobic basin to the anoxic basin.
- ammonium is converted into nitrates.
- This method has a constraint on the investment cost since it requires a large volume of expensive support materials.
- the limit of this treatment scheme is based on the quantity of sulphides to be oxidized by autotrophic denitrification, which consumes alkalinity.
- the proposed operating mode being a consumer of alkalinity (autotrophic nitrification in the aerated pool + autotrophic denitrification in the anoxic basin), in case of excess of sulphides to be treated, the anoxic environment would be limiting in alkalinity, or even in nitrates. The oxidation of sulphides would not be total.
- the production of volatile fatty acids in the first anaerobic reactor also consumes alkalinity, which is all the more unfavorable to the oxidation reactions of the sulfides in the second anoxic reactor.
- the object of the invention is, above all, to provide a process which makes it possible to eliminate the sulphides and the different forms of nitrogen in an economical and effective manner.
- the process according to the invention for the treatment of sulphide and ammonium-laden wastewater, in particular waste water of urban or industrial origin or digestion returns, condensates, leachates, is characterized in that:
- the wastewater first undergoes an anoxic treatment by biological means in free cultures according to which, in a first step, the organic carbon is essentially eliminated by heterotrophic bacteria, and in a second step, separated from the first, the sulphides are oxidized biologically by autotrophic bacteria with reduction of nitrates and / or nitrites,
- the effluent leaving the second stage is subjected to an aerobic biological treatment in free cultures for the conversion of ammonium to nitrates.
- a fraction of the effluent which has undergone the aerobic biological treatment in free cultures, and which contains nitrates, is recirculated to the second stage and the first stage of the anoxic treatment.
- the fraction of the effluent recirculated to the anoxic treatment is advantageously regulated as a function of the amount of sulphides to be treated.
- the S / N mass ratio (sulfur / nitrogen) is preferably maintained between 0.5 and 3.
- the recirculated fraction can be slaved to the amount of nitrates / nitrites needed to oxidize all the sulfides present in the water in the second stage of the anoxic treatment.
- the recirculated fraction is slaved to ensure, in the second step of the anoxic treatment, the mass ratio S / N (sulfur / nitrogen) of between 0.5 and 3.
- the oxidation of the sulfides biologically can be coupled to a sequential aerobic biological reactor (SBR) nitritation with a feed of the second stage of the anoxic nitrite treatment from nitrites.
- SBR sequential aerobic biological reactor
- Feeding the second stage of the anoxic nitrite treatment from the nitritation can be regulated depending on the amount of sulfide to be oxidized with the nitrites.
- the invention also relates to an installation for carrying out the process defined above, characterized in that it comprises two free-culture series biological reactors, the first reactor being a two-stage anoxic biological reactor comprising a heterotrophic basin. and a separate autotrophic basin, while the second reactor is an aerated basin in free cultures.
- a recirculation of nitrates is réatized from the aerated pool to the anoxic basins as a function of the concentration of sulphides to be oxidized.
- the nitrate recirculation can be carried out by stepped feeding or "step feed" from the aerated basin to the anoxic basins depending on the concentration of sulphides to be oxidized.
- the installation includes measurement probes in the anoxic basins and in the aerated basin for several parameters including the carbon content of the incoming effluent, and the sulphide content in the autotrophic anoxic basin, these measurement probes being connected to a controller which controls the recirculation flow rates according to the parameters measured.
- the sequential aerobic biological reactor can be coupled to the pond. anoxic autotrophic for a supply of nitrites from this basin.
- FIG. 2 is a diagram of an alternative embodiment of the installation.
- Fig.1 of the drawings there can be seen an installation according to the invention for the treatment, in a continuous flow, of wastewater loaded with sulphides and ammonium.
- This installation comprises an anoxic reactor 1 compartmentalized into a heterotrophic basin 1a followed by an autotrophic basin 1b.
- the two basins 1a and 1b are separated and the effluent leaving the basin 1a is taken up by pumping means and sent to the basin 1b.
- the pond 1a receives the flow Q of wastewater containing carbon, sulphides and ammonium.
- Aa, Ab agitation means are provided in each of the basins 1a, 1b. There is no insufflation of air or oxygen in these basins.
- Heterotrophic and autotrophic bacteria are naturally present in wastewater and in basins 1a, 1b, in the form of free cultures. Since the anoxic pool 1a receives a flow Q loaded with organic carbon, the heterotrophic bacteria grow rapidly in this pond 1a, while the autotrophic bacteria grow much less rapidly under such conditions.
- the anoxic basin 1a is thus heterotrophic and makes it possible to treat the incoming carbon, and to denitrify a surplus of nitrates coming from an aerated pond 2 and which are not used for the oxidation of the sulphides in the autotrophic anoxic basin 1b.
- the aerated pond 2 is located downstream of basin 1b
- the basin 1b receives the effluent exiting the basin 1a, effluent in which the organic carbon has been eliminated for the most part.
- the action of autotrophic bacteria in pond 1b is favored by the low organic carbon load of water from compartment 1a.
- the autotrophic anoxic basin 1b makes it possible to treat the sulphides present in the raw water by virtue of the nitrates originating from the aerated pool 2 and / or the nitrites resulting from the nitritation stage of the sequential aerobic biological reactor (SBR).
- Sulphides are oxidized by autotrophic denitrification which consumes alkalinity.
- Heterotrophic denitrification in basin 1a produces alkalinity. Thanks to this alkalinity production in the pond 1a, the process is not slowed down or stopped by a decrease in alkalinity due to the consumption in the basin 1b.
- the effluent from the basin 1b is sent, for an aerobic biological treatment in free cultures, in the aerated pond 2 which comprises agitating means Ac and aeration means B located in the bottom of the basin 2 for injecting bubbles. air or oxygen in the pool fluid.
- the aeration means B can be formed by perforated air blowing tubes or by nozzles installed in the floor or by any other conventional means.
- the biological treatment of water in reactor 2 results in nitrification and the conversion of ammonium NH 4 + to nitrate NO 3 " .
- the effluent leaving basin 2 contains sulphates SO 4 2" from sulfide oxidation from nitrates and / or nitrites.
- a recirculation duct 3 is provided between the ventilated tank 2 and the anoxic tank 1a, a pump 3p being mounted on the duct 3.
- a duct 4 is provided for the recirculation of the ventilated tank 2 to the anoxic tank 1b, a pump 4p being inserted in this conduit.
- the recirculation of the aerated tank 2 to the anoxic zones 1a, 1b to provide them with nitrates is therefore carried out in step feed or step-feed.
- the recirculation flow rate is slaved to the amount of nitrates necessary to oxidize all the sulphides present in the water in a ratio by mass S / N (sulfur / nitrogen) between 0.5 and 3.
- an automated controller 5 controls the operating speed, and therefore the flow rate, of the pumps 3p and 4p.
- the installation can include a series of flowmeters installed on the different ducts, and different sensors or measuring probes.
- the control instructions are established, in particular, according to parameters such as the organic carbon content in the incoming flow Q and in the heterotrophic anoxic basin 1a, the sulphide content in the incoming flow Q and in the autotrophic anoxic basin 1b and the nitrate content in the aerated pool 2. These parameters are obtained by measuring probes such as 6, 7 and 8 provided in the basins 1a, 1b, 2 and connected to the controller 5.
- Fig.2 is a diagram of an installation variant according to the invention in the case of a purification plant where there is a sludge die comprising an anaerobic digester (not shown) giving dehydration supernatants, loaded with nitrogen. These supernatants can be separately treated biologically in a SBR sequential aerobic biological reactor.
- the U flow of effluents, highly concentrated in N-NH 4 + of the centrates, filtrates, condensates and leachate type, is discharged into the reactor 9, which is a free culture aerated pond reactor with stirring means and insufflation means. air or oxygen in the bottom, as for the ventilated basin 2.
- the treatment of concentrated ammonium effluents is carried out by partial nitrification and denitrification.
- Ammonium is oxidized to nitrites which are reduced to gaseous nitrogen, without the need for nitrite to nitrates.
- This process also known as "nitrate shunt", described for example in EP-A-0826639, is theoretically capable of reducing by 25% the oxygen inputs for nitrification and by 40% the contributions of biodegradable carbonaceous reactants for denitrification, as well as the production of associated heterotrophic sludge.
- the elimination of effluents concentrated in nitrogen in the reactor 9 comprises several fractionated phases respectively feeding, aeration and anoxia, the number and the duration of these phases as well as the addition of carbon reactants being adjusted thanks to a series of real-time measurements in the effluent to be treated, in the discharge, and in the biological reactor 9.
- a supply of nitrites from the autotrophic anoxic reactor 1b is provided by a pipe 10 leaving the reactor 9 and opening into the reactor 1b.
- a pump 11, controlled by the controller 5, is arranged on the pipe 10.
- the reactor 1b feed is made from a fraction of the volume of water treated by the reactor 9 during the aerated phase during which there is production of nitrites. Part of these nitrites is sent to the basin 1b.
- the flow rate in line 10 is controlled according to the need for nitrites to oxidize the sulfides in the autotrophic anoxic reactor 1b.
- concentration ranges of the different physico-chemical parameters during the treatment described in the scheme of FIG. 1 are:
- the anoxic reactors 1a and 1b have a mechanical stirring system and the ventilated tank 2 of an air blowing system in addition to mechanical agitation.
- the concentration of suspended solids in basins 1a, 1b and 2 is maintained between 1 and 5 g / l.
- the step-feed recirculation rate is a function of the concentration of nitrates and sulphides and varies between 50 and 400%.
- the pH is between 6.5 and 8.5.
- the sludge age in pools is between 6 and 20 days, depending on the temperature.
- the hydraulic residence time or TSH in each of the reactors 1a and 1b is 2 to 3h and in the reactor 2 from 4 to 6h.
- Two basins 1a and 1b each with a TSH of 2h and a pool 2 with a TSH of 4h.
- the ratio of sulphides to be eliminated / nitrates consumed chosen is 1, 5. Under these conditions, in order to oxidize 30 mg / l of sulphides, 20 mg / l of N-NO 3 "is required . * The nitrate recirculation from basin 2 to basin 1b must allow this concentration to be brought in. Excess nitrates , ie 25 mg / l, are denitrified by recirculation in pond 1a.
- the proposed system is capable of removing 100% of the sulphides present in the raw water, nitrifying and denitrifying completely.
- the S / N ratio of 1.5 is no longer respected because there is a deficit of nitrates due to a low ammonium concentration at the input station. It is always necessary to have 20 mg / l of N-NOx to oxidize the 30 mg / l of sulphides. In the present case, it has been chosen to recirculate 50% of the outflow from the aerated tank 2 to the anoxic hetérotrophe basin 1a, ie 5 mg / l of N-NOx, since it is essential to recover TAC (complete alkalimetric titre). for autotrophic denitrification. 15 mg / l of N-NOx are missing which can be compensated for by the fraction of the volume of treated water supplied by the reactor 9.
- the invention allows treatment of wastewater virtually without consuming expensive chemical reagents, and with reduced sludge production due to the low growth of autotrophic bacteria in the autotrophic anoxic basin.
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- Biodiversity & Conservation Biology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Health & Medical Sciences (AREA)
- Molecular Biology (AREA)
- Purification Treatments By Anaerobic Or Anaerobic And Aerobic Bacteria Or Animals (AREA)
Abstract
Description
Claims
Priority Applications (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
AU2008244181A AU2008244181B2 (en) | 2007-03-02 | 2008-02-27 | Method and equipment for processing waste water containing sulphides and ammonium |
MX2009009315A MX2009009315A (es) | 2007-03-02 | 2008-02-27 | Proceso e instalacion para tratamiento de aguas residualers que contienen sulfuros y amonio. |
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0701534 | 2007-03-02 | ||
FR0701534A FR2913234B1 (fr) | 2007-03-02 | 2007-03-02 | Procede et installation de traitement d'eaux usees contenant des sulfures et de l'ammonium. |
Publications (2)
Publication Number | Publication Date |
---|---|
WO2008132296A2 true WO2008132296A2 (fr) | 2008-11-06 |
WO2008132296A3 WO2008132296A3 (fr) | 2009-01-08 |
Family
ID=38668823
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
PCT/FR2008/000255 WO2008132296A2 (fr) | 2007-03-02 | 2008-02-27 | Procede et installation de traitement d'eaux usees contenant des sulfures et de l'ammonium |
Country Status (5)
Country | Link |
---|---|
CN (1) | CN101626983A (fr) |
AU (1) | AU2008244181B2 (fr) |
FR (1) | FR2913234B1 (fr) |
MX (1) | MX2009009315A (fr) |
WO (1) | WO2008132296A2 (fr) |
Cited By (7)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101987770A (zh) * | 2010-08-07 | 2011-03-23 | 中国石油化工股份有限公司 | 一种脱除油田回注水中的硫化氢的方法 |
CN103496827A (zh) * | 2013-10-12 | 2014-01-08 | 常州大学 | 一种酸性羧甲基纤维素冷凝液的处理方法 |
CN103910467A (zh) * | 2014-05-14 | 2014-07-09 | 苏州市阳澄湖现代农业产业园特种水产养殖有限公司 | 一种水产养殖废水的处理方法 |
CN104843953A (zh) * | 2015-06-08 | 2015-08-19 | 河南工业大学 | 电化学与生物氢自养协同作用深度转化水中高氯酸盐的方法和反应器 |
WO2020231245A1 (fr) | 2019-05-13 | 2020-11-19 | Université Sidi Mohamed Ben Abdellah | Installation de traitement des lixiviats des décharges contrôlées |
EP3582881A4 (fr) * | 2017-02-15 | 2020-12-23 | General Electric Company | Régulation d'oxydation destinée au perfectionnement de l'efficacité de désulfuration de gaz de combustion |
WO2022175387A1 (fr) * | 2021-02-22 | 2022-08-25 | Meudal Nicolas | Procédé étagé de traitement d'effluents aqueux |
Families Citing this family (6)
Publication number | Priority date | Publication date | Assignee | Title |
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CN101863592B (zh) * | 2010-06-21 | 2011-11-30 | 浙江大学 | 一种城镇小型生活垃圾填埋场渗滤液处理方法 |
US9884779B2 (en) * | 2010-12-02 | 2018-02-06 | The Hong Kong University Of Science And Technology | Biological wastewater treatment and reuse utilizing sulfur compounds as electron carrier to minimize sludge production |
WO2015198279A1 (fr) | 2014-06-26 | 2015-12-30 | Degremont | Procede et installation de traitement biologique des sulfures et des composes soufres dans les eaux residuaires |
FR3022903B1 (fr) * | 2014-06-26 | 2020-06-05 | Degremont | Procede et installation de traitement biologique des sulfures et des composes soufres dans les eaux residuaires |
MD4483C1 (ro) * | 2016-12-19 | 2017-12-31 | Василий ВЫРЛАН | Instalaţie şi procedeu de epurare a apelor uzate şi încărcătură flotantă |
CN106865887A (zh) * | 2017-02-22 | 2017-06-20 | 浙江华建尼龙有限公司 | 尼龙切片生产废水及生活污水混合处理系统及其处理方法 |
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US5705072A (en) * | 1997-02-03 | 1998-01-06 | Haase; Richard Alan | Biotreatment of wastewater from hydrocarbon processing units |
GB2369115A (en) * | 2000-11-17 | 2002-05-22 | Kwangju Inst Sci & Tech | Simultaneous removal process of nitrogen and phosphorus in wastewater |
FR2841548A1 (fr) * | 2002-06-28 | 2004-01-02 | Syndicat Interdepartemental Po | Procede de traitement en trois etapes biologiques d'un effluent |
WO2005033019A1 (fr) * | 2003-09-30 | 2005-04-14 | O.K. Technologies, Llc | Chambre de denitration autotrophe sur soufre et reacteur a calcium |
WO2006113560A2 (fr) * | 2005-04-15 | 2006-10-26 | Bion Environmental Technologies, Inc. | Elimination de nutriments par voie biologique dans un environnement pauvre en oxygene |
-
2007
- 2007-03-02 FR FR0701534A patent/FR2913234B1/fr not_active Expired - Fee Related
-
2008
- 2008-02-27 AU AU2008244181A patent/AU2008244181B2/en not_active Expired - Fee Related
- 2008-02-27 MX MX2009009315A patent/MX2009009315A/es not_active Application Discontinuation
- 2008-02-27 CN CN200880006891A patent/CN101626983A/zh active Pending
- 2008-02-27 WO PCT/FR2008/000255 patent/WO2008132296A2/fr active Application Filing
Patent Citations (5)
Publication number | Priority date | Publication date | Assignee | Title |
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US5705072A (en) * | 1997-02-03 | 1998-01-06 | Haase; Richard Alan | Biotreatment of wastewater from hydrocarbon processing units |
GB2369115A (en) * | 2000-11-17 | 2002-05-22 | Kwangju Inst Sci & Tech | Simultaneous removal process of nitrogen and phosphorus in wastewater |
FR2841548A1 (fr) * | 2002-06-28 | 2004-01-02 | Syndicat Interdepartemental Po | Procede de traitement en trois etapes biologiques d'un effluent |
WO2005033019A1 (fr) * | 2003-09-30 | 2005-04-14 | O.K. Technologies, Llc | Chambre de denitration autotrophe sur soufre et reacteur a calcium |
WO2006113560A2 (fr) * | 2005-04-15 | 2006-10-26 | Bion Environmental Technologies, Inc. | Elimination de nutriments par voie biologique dans un environnement pauvre en oxygene |
Cited By (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
CN101987770A (zh) * | 2010-08-07 | 2011-03-23 | 中国石油化工股份有限公司 | 一种脱除油田回注水中的硫化氢的方法 |
CN103496827A (zh) * | 2013-10-12 | 2014-01-08 | 常州大学 | 一种酸性羧甲基纤维素冷凝液的处理方法 |
CN103496827B (zh) * | 2013-10-12 | 2015-05-20 | 常州大学 | 一种酸性羧甲基纤维素冷凝液的处理方法 |
CN103910467A (zh) * | 2014-05-14 | 2014-07-09 | 苏州市阳澄湖现代农业产业园特种水产养殖有限公司 | 一种水产养殖废水的处理方法 |
CN104843953A (zh) * | 2015-06-08 | 2015-08-19 | 河南工业大学 | 电化学与生物氢自养协同作用深度转化水中高氯酸盐的方法和反应器 |
CN104843953B (zh) * | 2015-06-08 | 2017-07-18 | 河南工业大学 | 电化学与生物氢自养协同作用深度转化水中高氯酸盐的方法 |
EP3582881A4 (fr) * | 2017-02-15 | 2020-12-23 | General Electric Company | Régulation d'oxydation destinée au perfectionnement de l'efficacité de désulfuration de gaz de combustion |
WO2020231245A1 (fr) | 2019-05-13 | 2020-11-19 | Université Sidi Mohamed Ben Abdellah | Installation de traitement des lixiviats des décharges contrôlées |
WO2022175387A1 (fr) * | 2021-02-22 | 2022-08-25 | Meudal Nicolas | Procédé étagé de traitement d'effluents aqueux |
FR3120072A1 (fr) * | 2021-02-22 | 2022-08-26 | Nicolas Meudal | Procédé étagé de traitement d’effluents aqueux |
Also Published As
Publication number | Publication date |
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AU2008244181B2 (en) | 2012-02-02 |
FR2913234A1 (fr) | 2008-09-05 |
WO2008132296A3 (fr) | 2009-01-08 |
MX2009009315A (es) | 2009-09-10 |
CN101626983A (zh) | 2010-01-13 |
AU2008244181A1 (en) | 2008-11-06 |
FR2913234B1 (fr) | 2009-05-08 |
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