Classifications

• • 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
  • C02F1/008—Control or steering systems not provided for elsewhere in subclass C02F
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
  • B01D61/025—Reverse osmosis; Hyperfiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
  • B01D61/027—Nanofiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
  • B01D61/04—Feed pretreatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/02—Reverse osmosis; Hyperfiltration ; Nanofiltration
  • B01D61/12—Controlling or regulating
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/145—Ultrafiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/147—Microfiltration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/16—Feed pretreatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D61/00—Processes of separation using semi-permeable membranes, e.g. dialysis, osmosis or ultrafiltration; Apparatus, accessories or auxiliary operations specially adapted therefor
  • B01D61/14—Ultrafiltration; Microfiltration
  • B01D61/22—Controlling or regulating
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
  • B01D65/02—Membrane cleaning or sterilisation ; Membrane regeneration
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2311/00—Details relating to membrane separation process operations and control
  • B01D2311/04—Specific process operations in the feed stream; Feed pretreatment
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2321/00—Details relating to membrane cleaning, regeneration, sterilization or to the prevention of fouling
  • B01D2321/16—Use of chemical agents
  • B01D2321/168—Use of other chemical agents
• • B—PERFORMING OPERATIONS; TRANSPORTING
  • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
  • B01D—SEPARATION
  • B01D2325/00—Details relating to properties of membranes
  • B01D2325/26—Electrical properties
• • 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
  • C02F1/44—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis
  • C02F1/444—Treatment of water, waste water, or sewage by dialysis, osmosis or reverse osmosis by ultrafiltration or microfiltration
• • 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
  • C02F1/52—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities
  • C02F1/5236—Treatment of water, waste water, or sewage by flocculation or precipitation of suspended impurities using inorganic agents
• • 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
  • C02F2209/02—Temperature
• • 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
  • C02F2209/03—Pressure
• • 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

Definitions

• the present invention relates to a method of optimized management of a membrane filtration unit, as a function of the fouling state of the membrane and / or the temperature, implementing a membrane microcoagulation according to the patent EP 1 239 943, from the application WO 01/41906, which the applicant holds.
• Microcoagulation involves injecting upstream of the membrane a dose of coagulation reagent (s) 30 to 80 times lower than the dose of reagent (s) canceling the Zeta potential of the effluent.
• the hydraulic performances of a membrane are illustrated by its permeability, ie the flow of effluent passing a unitary surface of membrane for a pressure difference applied on both sides of the standardized membrane of 1 bar at a given temperature.
• Initial permeability or Lpi the measurement of the permeability of a new membrane made on drinking water whose clogging index and temperature must be completed.
• the treatment unit must be dimensioned for the coldest temperature, that is, when this minimum temperature is below 20 ° C., it is necessary to increase accordingly. the membrane surface installed.
• Lp @ T ° reference K * Lp @ T ° with K a function of the temperature of the effluent and the reference temperature. This reference temperature is currently set at 20 or 25 ° C.
• Clogging Under the generic term clogging, well documented in the literature, the skilled person refers to all phenomena that increase the resistance of the membrane either mechanically or chemically. This concerns the surface deposits (cake formation), adsorption phenomena on the membrane and in the pores of the membrane, phenomena in which the various substances contained in the water are involved: suspended solids and colloids, organic and mineral materials.
• this clogging involves: - either a decrease in the filtration flow for a constant applied transmembrane pressure
• Lpi value of the initial membrane permeability during its first implementation
• Control of this clogging is therefore a major challenge perfectly identified by the skilled person who proposes a panel of solutions to prevent clogging (preventive measures) which, when it occurs, can be eliminated only by curative measures .
• the curative measures are essentially chemical washes of the membrane detailed in the literature. These measures mainly consist of arranging phases of contact of the membrane with a washing solution which may contain one or more chemical reagents of the acidic and / or chelating, detergent, oxidizing, etc. type.
• these healing phases is subject to a finding of clogging of the membrane, ie a measure of permeability below a threshold set by the supplier of said membrane for example.
• these curative measures can be practiced as a preventive measure with a given frequency, for example 1 time / month to 1 time / year.
• preventive measures must be implemented continuously or associated with carefully chosen triggering factors, generally the quality of the effluent, to anticipate the phenomena of clogging. Indeed, when the clogging is proven (in particular by observation of a drop in permeability), preventive measures have no effect and only the curative measures can restore the hydraulic performance of the membrane.
• EP 1 239 943 and WO 01/41906 which describe a chemical microcoagulation process for improving the production capacity of a membrane.
• This membrane microcoagulation process consists in injecting, upstream of the membrane, a dose Y of coagulation reagent (s) 30 to 80 times lower, and alternatively 40 to 60 times lower, at the dose X of reagent (s). canceling the Zeta potential of the effluent.
• Y is between X / 30 and X / 80, alternatively between X / 40 and X / 60.
• the coagulation reagent (s) is known to those skilled in the art as having no cleaning properties for the membrane.
• Microcoagulation according to EP 1 239 943 can be implemented continuously but this implementation is not always necessary or desirable and, in any case, not optimized technically and economically. On the one hand, in the absence of risk of clogging of the membrane, the implementation of microcoagulation is not necessarily necessary and may lead to unnecessary reagent costs.
• the invention aims in particular to optimize the duration of implementation of the microcoagulation and thus to preserve the life of the membrane, which is of great technical and economic interest.
• the objective of the invention is to optimize the management of the implementation of membrane microcoagulation, a preventive measure, as a function of the return of operation of the membrane installation, that is to say according to the only measurement of the permeability, without the addition of additional sensors of effluent quality or other. Only sensors will be used, which are usually present as standard on membrane installations (measurement of temperature, filtration rate and transmembrane pressure).
• Another objective of the present invention is to optimize the implementation of microcoagulation to obtain constant hydraulic performance of the membrane over time.
• the present invention describes an optimized, reliable and secure method of driving a membrane filtration unit and opens the way to a new concept which is that of the isoflux membrane and / or isopermeability @ T.
• microcoagulation membrane described by EP 1 239 943 appears as a preventive procedure
• the inventor has found that, quite surprisingly, microcoagulation induces a restoration of the performance of a clogged membrane. Without intervention of microcoagulation, the Clogged membrane would have required a so-called curative wash phase of chemical washing. This particularly surprising observation is quite new.
• the management of the implementation of the resulting microcoagulation on membrane is equally surprising by recommending the use of a triggering factor of curative measures (finding of fouling) for the successful implementation of preventive measures (the microcoagulation on membrane).
• the method of optimized management of a membrane filtration unit implementing membrane microcoagulation comprising at least:
• the injection of the coagulation reagent (s) is controlled when the permeability of the membrane becomes lower than a threshold value
• the permeability of the membrane can be corrected at a reference temperature, and the threshold value of the permeability is between 10 and 80% of the initial permeability of the membrane at said reference temperature, while the stopping of the injection of the coagulation reagent (s) is controlled when the permeability of the membrane, corrected at the reference temperature, becomes equal to or greater than the stable value of the permeability LpO before decreasing to the reference temperature for a time determined maintenance.
• the threshold value corresponds to a decrease of 10 to 40% in the permeability of the membrane, corrected at a reference temperature, over a fixed time step, and stopping the injection of the coagulation reagent (s) is controlled when the permeability of the membrane, corrected to the reference temperature, becomes equal to or greater than the stable value of permeability LpO before reduction to the said reference temperature.
• the injection of the coagulation reagent (s) can be controlled by a decrease in the permeability of the membrane, at the actual temperature of the effluent, below a threshold value of between 10 and 80% of the initial permeability Lpi of the membrane at the said temperature of the effluent, and the stop of the injection of the reagent (s) of coagulation is controlled when the permeability of the membrane, at the actual temperature of the effluent, again becomes equal to or greater than the stable value of the permeability LpO at the temperature of the effluent before reduction.
• the threshold value can correspond to a decrease of 10 to 40% of the permeability of the membrane, to the actual temperature of the effluent, on a fixed time step, and the stop of the injection of the reagent ( s) coagulation is controlled when the permeability of the membrane at the actual temperature of the effluent becomes equal to or greater than the stable value of the permeability LpO before reduction at the temperature of the effluent.
• the reference temperature is usually 20 or 25 ° C.
• the time step set for the evolution of the permeability may be between 10 min and 5 d, preferably between 10 and 60 min.
• the stop of the injection of the coagulation reagent (s) can be controlled when the permeability of the membrane becomes, and remains, equal to or greater than the stable value of the permeability LpO before decrease during a longer hold time at twelve o'clock.
• the invention also relates to an installation for the optimized management of a membrane filtration unit with membrane microcoagulation, comprising at least: a means for measuring the temperature of the effluent,
• means for measuring the transmembrane pressure for the implementation of a method as defined above, characterized in that it comprises a means for controlling the injection of the coagulation reagent (s). connected to the means for measuring the temperature of the effluent, the filtration flow rate, and the transmembrane pressure, this control means being provided for: determine the permeability of the membrane and compare it with a threshold value,
• the invention proposes, in particular, to trigger the implementation of microcoagulation on the observation:
• This threshold is advantageously between 10 and 80% of the value of the initial permeability of the membrane at said reference temperature
• This threshold is advantageously set between 10 and 40% of the value of the permeability at said reference temperature over a time step of 10 min to 5 d of filtration.
• microcoagulation membrane In addition to the surprising curative effect of the implementation of microcoagulation membrane, another finding of the inventor is that the effect of improving the hydraulic performance of the membrane can advantageously be exploited to compensate for the negative effect of a drop in temperature on the hydraulic performance of the membrane, application never described.
• the judicious implementation of microcoagulation allows a new and surprising way to overcome a fundamental law of physics hitherto suffered by operators of membrane technologies.
• the implementation of the microcoagulation allows according to the present invention to erase the negative effect of a drop in temperature and / or an increase in the clogging character of the effluent.
• the management of the implementation of the membrane microcoagulation allows a relevant discontinuous operation of said process and judiciously restrict the implementation of said method to the only periods when its implementation is necessary. In this, this management allows savings of reagents and advantageously preserve the life of the membrane.
• Another advantage of the present invention is that it does not require the addition of any equipment that is not present on the membrane filtration plants, namely the measurement of the effluent temperature, the filtration rate and the measurement of the temperature. the transmembrane pressure from which the permeability at the temperature of the effluent and / or at a reference temperature is calculated.
• the present invention does not induce investment cost or maintenance of additional sensors, or the always difficult choice of said sensors depending on the nature of the effluent that are specific to each site, which would complicate exercise.
• Fig. 1 is a diagram of an installation with a crankcase membrane in circulation implementing the method according to the invention.
• Fig. 2 is a diagram of an installation with membrane without immersed housing implementing the method according to the invention.
• Fig. 3 is a diagram illustrating the evolution of the hydraulic performance of a membrane and the concentration in organic pollution of the effluent over time, according to Example 1, and
• Fig. 4 is a diagram illustrating the evolution of the hydraulic performance of a membrane and the quality of the effluent as a function of time, according to Example 2.
• Fig. 4 is a diagram illustrating the evolution of the hydraulic performance of a membrane and the quality of the effluent as a function of time, according to Example 2.
• identical or similar elements have been designated by the same references.
• the coagulating reagent is injected at 2, upstream of the membrane into the water to be treated.
• the water to be treated-coagulating reagent is then filtered on the membrane in the housing.
• the installation optionally comprises a recirculation loop 5.
• the treated water 3 exits via a pipe.
• the coagulating reagent is injected at 2, upstream of the membrane into the water to be treated 1.
• the water-to-treated-coagulating reagent mixture is then filtered on the membrane 6, without a housing, immersed in a basin containing the water to be treated.
• the treated water 3 is evacuated using a pump P.
• the dose Y of coagulation reagent (s) injected into the water to be treated 1, upstream of the membrane, is 30 to 80 times lower, and alternatively 40 to 60 times lower, at the dose X of reagent canceling the potential.
• Zeta of the water to be treated 1. Y is therefore between X / 30 and X / 80, alternatively between X / 40 and X / 60.
• the installation comprises a control unit U, in particular constituted by a computer or a programmable controller. Measuring sensors are connected to this unit U to transmit information on operating parameters.
• the installation comprises at least: a sensor 7 for measuring the temperature of the effluent 1,
• a sensor 8 of the filtration flow rate installed on the exit pipe of the treated water 3,
• one or more sensors 9 for measuring the transmembrane pressure are connected to the unit U which determines, from the measurement results provided, the instantaneous permeability of the membrane.
• a valve 10, installed on the inlet pipe of the reagent 2, is controlled by the unit U in which is loaded a program, constituting the injection control means, and according to which: the injection of the reagent (s), by opening the valve 10, is controlled when the permeability of the membrane, possibly corrected at a reference temperature, becomes less than a threshold value included between 10 and 80% of the initial permeability of the membrane at said reference temperature,
• This holding time is preferably greater than 12 hours.
• the reference temperature is usually 20 or 25 ° C.
• the threshold value corresponds to a decrease of 10 to 40% in the permeability of the membrane, possibly corrected at a reference temperature, over a fixed time step, and stopping the injection of the Coagulation reagent (s) is controlled when the permeability of the membrane, possibly corrected at the reference temperature, becomes equal to or greater than the value of the permeability LpO before decrease.
• the fixed time step for the evolution of the permeability triggering the implementation of the microcoagulation is generally between 10 min and 5 d
• This first example concerns the filtration of karstic water by an industrial ultrafiltration unit with a production capacity of 2,000 m 3 / d. It is a hollow fiber-type membrane in casing whose initial permeability Lpi is 300 L / hm 2 .bar @ 20 ° C measured on a drinking water whose clogging index (ie SDI) is 5 % / min measured according to ASTM D 4189.95.
• FIG. 3 illustrates the evolution of the hydraulic performances of the membrane as a function of time, plotted on the abscissa and expressed in hours, and the concentration in organic pollution.
• the permeability expressed in L / hm 2 .bar @ 20 ° C is plotted on the ordinate with the graduations on the left scale.
• the flux expressed in L / hm 2 @ 20 c C is plotted on the ordinate with graduations on the left scale.
• the UV absorbance at 254 nm (m -1 ) of the effluent to be treated is plotted on the ordinate with graduations on the scale of right and is represented by vertical bands corresponding to measurement periods (average sample over 24 hours).
• the resource whose characteristics are summarized in Table 1 below, is a cold water (temperature of 8 ° C), slightly turbid which, for reasons poorly known to date undergoes sudden increases in organic pollution during the rainy episodes. This pollution is illustrated by a very significant increase in the measurement of the UV absorbance at 254 nm, greater than 15 m -1 , significant of an increase in the concentration of large unsaturated organic molecules. Excluding rainfall events, the UV254 nm absorbance measurement is relatively constant at a level of 2 to 4 m- 1 .
• the implementation of the microcoagulation is triggered while the permeability dropped to the threshold value of 120 L / hm 2 @ 20 ° or - a threshold value equivalent to 34% of the Lpi (120/350), - a further decrease of 30% in 96h of stable permeability
• microcoagulation is stopped.
• the Microcoagulation is handed out to the 350th hour and similar impacts on the evolution of the permeability are reproduced.
• the example reported below relates to a test carried out on a pilot ultrafiltration unit.
• the initial permeability of the membrane Lpi is 350 L / hm 2 .bar @ 20 ° C, ie after correction of the temperature approximately 270 L / hm 2 .bar @ 10 ° C (measurement carried out with drinking water including the SDI is 6% / min according to ASTM
• the experiment was carried out on Seine water whose temperature was naturally 20 ° C. and punctually cooled to 10 ° C. using a cold group for the purposes of the experiment.
• the quality of the Seine water during the test is as follows:
• FIG. 4 The results of the experiment discussed below are illustrated by FIG. 4.
• the flux applied to the membrane is constant and set at 70 L / hm 2 @ T.
• the flow measurement points are represented by crosses in Fig.4.
• the temperature measurement points are represented by squares, while the measurement points of the absorbance are represented by full circles.
• the permeability measuring points are represented by diamonds.
• Fig.4 the time is plotted on the abscissa.
• the permeability expressed in L / hm 2 .bar @ T ° C is plotted on the ordinate with graduations on the left scale.
• the flux expressed in L / hm 2 @ T ° C is plotted on the ordinate with graduations on the left scale.
• the UV absorbance at 254 nm (m 1 ) of the effluent to be treated is plotted on the ordinate with graduations on the right scale.
• the temperature is plotted on the ordinate with graduations on the right scale.
• the temperature of the effluent is 20 0 C and the membrane is new.
• the permeability of the membrane naturally decreases from its initial value Lpi of 350 L / hm 2 .bar @ 20 ° C and stabilizes at an LpO value of 250 L / hm 2 .bar @ 20 ° C, in this case # 71% of the initial permeability of the membrane @ 20 ° C (250 # 0.71 * 350).
• the Seine water is cooled with a cold group at a temperature of 10 ° C.
• the impact of the drop in temperature on the viscosity of the water then induces a Gradual decrease in permeability of the order of 23 to 25% according to the state of the art while the characteristics of the Seine water, in particular the level of organic pollution, remains constant.
• the permeability measurement then stabilizes at a level of 190 l / hm 2 .bar @ T.
• the microcoagulation membrane is implemented according to the invention during phase 3 of the test.
• the inventor observes a restoration of the performance of the membrane at 10 0 C at a level similar to that obtained for an effluent at 20 ° C.
• the permeability at 20 ° C. in the absence of the microcoagulation is then similar to the permeability at 10 ° C. 0 C with membrane microcoagulation, ie 250 L / hm 2 .bar.
• phase 4 the cooling of the effluent was stopped and the implementation of the membrane microcoagulation suspended for a fortnight (phase 4) pending a natural degradation of the quality of the effluent. the resource.
• phase 5 this degradation occurred with an increase in organic pollution, increase in TOC value from 3 to 5 mg C / L, increase in UV254 nm absorbance by 3-4 m -1 at 5-7 m "1 .
• Such variations on this resource are significant to a real increase in the clogging potency of the effluent.
• FIG. 4 then illustrates the surprising restoration of the permeability of the membrane, at the value of 250 L / hm 2 .bar @ 10 ° C, at the temperature of the effluent with a maintenance of performances now similar to those obtained with a water less clogging and at a much higher temperature throughout the phase 6 of the test.
• This example illustrates the potential to manage the onset of membrane microcoagulation implementation on the measurement of permeability at the actual effluent temperature, thus clearing and offsetting the effects of clogging and / or decay. of the temperature.
• This management opens up new perspectives for stabilizing the operation of an ultrafiltration unit and tending towards isoflux and isopermeability throughout the year.
• the invention does not involve a specific stoppage of the production process, except alternating filtration / backwashing.
• the coagulation reagents used are not washing reagents or reagents having oxidizing or disinfecting properties.

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• Engineering & Computer Science (AREA)
• Water Supply & Treatment (AREA)
• Chemical & Material Sciences (AREA)
• Chemical Kinetics & Catalysis (AREA)
• Nanotechnology (AREA)
• Life Sciences & Earth Sciences (AREA)
• Hydrology & Water Resources (AREA)
• Environmental & Geological Engineering (AREA)
• Organic Chemistry (AREA)
• Separation Using Semi-Permeable Membranes (AREA)
• Separation Of Suspended Particles By Flocculating Agents (AREA)

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• 2006
  • 2006-12-19 FR FR0611072A patent/FR2909903B1/fr not_active Expired - Fee Related
• 2007
  • 2007-12-14 RU RU2009127745/05A patent/RU2415696C2/ru not_active IP Right Cessation
  • 2007-12-14 US US12/519,689 patent/US20100032373A1/en not_active Abandoned
  • 2007-12-14 CA CA002672769A patent/CA2672769A1/fr not_active Abandoned
  • 2007-12-14 CN CNA2007800496876A patent/CN101588858A/zh active Pending
  • 2007-12-14 EP EP07871865A patent/EP2104551A2/de not_active Withdrawn
  • 2007-12-14 AU AU2007344318A patent/AU2007344318B2/en not_active Ceased
  • 2007-12-14 WO PCT/FR2007/002074 patent/WO2008087300A2/fr active Application Filing
  • 2007-12-14 JP JP2009542130A patent/JP2010513009A/ja active Pending

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