WO2008132186A1 - Systeme et procede de commande de surveillance pour nettoyage de membrane - Google Patents

Systeme et procede de commande de surveillance pour nettoyage de membrane Download PDF

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Publication number
WO2008132186A1
WO2008132186A1 PCT/EP2008/055113 EP2008055113W WO2008132186A1 WO 2008132186 A1 WO2008132186 A1 WO 2008132186A1 EP 2008055113 W EP2008055113 W EP 2008055113W WO 2008132186 A1 WO2008132186 A1 WO 2008132186A1
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Prior art keywords
membrane
fouling
cleaning
permeate
reversible
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PCT/EP2008/055113
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English (en)
Inventor
Etienne Brauns
Erwin Van Hoof
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Vlaamse Instelling Voor Technologisch Onderzoek (Vito)
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Publication of WO2008132186A1 publication Critical patent/WO2008132186A1/fr

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    • 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
    • B01D61/22—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
    • B01D65/00—Accessories or auxiliary operations, in general, for separation processes or apparatus using semi-permeable membranes
    • B01D65/08—Prevention of membrane fouling or of concentration polarisation
    • 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
    • C02F3/02—Aerobic processes
    • C02F3/12—Activated sludge processes
    • C02F3/1236—Particular type of activated sludge installations
    • C02F3/1268—Membrane bioreactor systems
    • C02F3/1273—Submerged membrane bioreactors
    • 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
    • B01D2321/18—Use of gases
    • B01D2321/185—Aeration
    • 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
    • C02F1/5209—Regulation methods for flocculation or precipitation
    • 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
    • C02F1/72—Treatment of water, waste water, or sewage by oxidation
    • C02F1/76—Treatment of water, waste water, or sewage by oxidation with halogens or compounds of halogens
    • 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
    • C02F2209/22—O2
    • 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
    • C02F2209/36—Biological material, e.g. enzymes or ATP
    • 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
    • C02F2209/38—Gas 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
    • C02F2209/40—Liquid flow rate
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2303/00—Specific treatment goals
    • C02F2303/16—Regeneration of sorbents, filters
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2305/00—Use of specific compounds during water treatment
    • C02F2305/04—Surfactants, used as part of a formulation or alone
    • 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 present invention is related to membrane filtration systems and to the cleaning of the membranes of said systems. More particularly, the present invention is related to pressure-driven membrane filtration systems.
  • Membranes are used in filtration processes in order to clean liquids from contaminants and/or solid particles.
  • a feed is separated into a "clean" filtrate fraction (i.e. the permeate) and a concentrated fraction as a result of a pressure difference across the membrane surface.
  • the separation process is mechanical since the pores within the membrane act as a physical barrier towards constituents which are larger than the pores. As a result, at least all particles which are larger than those pores are withheld from the feed that is passing through the membrane. Due to a build-up of retained compounds at the membrane surface during filtration, deposition onto the membrane and obstruction of the membrane pores will take place to various extents.
  • the cleaning of waste water can be done in a very efficient way in a membrane bioreactor (MBR) at a high sludge concentration (called mixed liquid suspended solids or MLSS) while removing effluent through membrane filtration.
  • MBR membrane bioreactor
  • MLSS mixed liquid suspended solids
  • the production of the MBR effluent is done by using a membrane.
  • the membrane permeate constitutes the MBR effluent while the concentrate is remixed within the biomass (sludge) itself.
  • Membrane fouling consists of extremely complex phenomena. Different types of fouling mechanisms act in parallel since there are numerous fouling constituents, e.g. particles, dissolved inorganics, dissolved organics, bacteria and floes, colloids and coagulated constituents. They interact with the membrane surface and membrane pores in very complex ways. The fouling constituents also interact with one another.
  • Membrane filtration systems of the prior art are equipped with a lower-level control system (e.g. PLC) in which specific parameter values, which are related to the mechanical and/or the chemical cleaning, are set according to the experience of a human programmer. Generally, these parameter values are only adjusted on an occasional basis. Hence, the operation of the membrane filtration system may not be optimized in cases in which the feed has a varying fouling propensity (which is the case in e.g. municipal waste water systems) . In a large number of cases the cleaning results to be performed either too often or too seldom and hence does not take into account the actual fouling propensity of the treated sludge. This results in membrane filtration systems which operate in a less optimized and less efficient way.
  • PLC lower-level control system
  • a few measurement devices have been developed, which may give an indication of the fouling propensity of a sludge that may be applied as a feed to a membrane filtration system. These measurement devices however, either are not suitable to be used in an on-line or continuous measurement, or measure only a specific kind of fouling constituents present in the sludge, or they measure the total fouling propensity of the sludge.
  • the latter fouling measurement method is hence restricted to the dead-end measurement of the total fouling propensity of a sludge.
  • An indication on the total fouling propensity of a sludge is however of limited practical use for steering the membrane cleaning actions, as these would need a distinction to be made between mechanical and chemical cleaning, which are related to distinct fouling types.
  • the present invention aims to optimize the efficiency of a membrane filtration system. It is an aim of the invention to provide an automated and optimized control of membrane cleaning actions in a membrane filtration system, thereby obviating the shortcomings of the prior art. It is an aim of the invention to separately and individually optimize the control of the mechanical and chemical cleaning actions in a membrane filtration system. [0013] It is a further aim of the present invention to provide a membrane filtration system which operates at higher efficiency compared to membrane filtration systems of the prior art. The present invention aims to provide a system for controlling the mechanical and/or chemical membrane cleaning actions separately and automatically.
  • a method of controlling membrane cleaning actions of a membrane filtration system comprises a step of providing a device for measuring a fouling propensity of a feed applied to (membranes of) the membrane filtration system, wherein the device comprises a permeate production facility comprising a membrane.
  • the method further comprises a step of feeding at least a part of the feed to the membrane of said permeate production facility.
  • the method further comprises a step of applying a trans- membrane-pressure across the membrane of said permeate production facility for producing permeate in cross-flow.
  • the method further comprises a step of measuring the (volume) rate of permeate produced by said permeate production facility in function of time in a first measuring step.
  • the method further comprises a step of iteratively performing the steps of cleaning the membrane of said permeate production facility by at least one mechanical cleaning action, followed by measuring the rate of permeate produced by said permeate production facility in function of time.
  • the method further comprises a step of computing a reversible fouling propensity of the feed based on the rate of permeate which is recovered after each cleaning step.
  • the method further comprises a step of computing an irreversible fouling propensity of said feed based on the rate of permeate which remains unrecovered after each cleaning step.
  • the method further comprises a step of calculating the value of at least one first parameter related to a membrane cleaning action based on the reversible fouling propensity.
  • the method preferably further comprises a step of calculating the value of at least one second parameter related to a membrane cleaning action based on the irreversible fouling propensity.
  • Said first and second parameters form part of a set of parameters related to membrane cleaning actions of the membrane filtration system.
  • the step of feeding at least a part of the feed to the membrane of the permeate production facility comprises providing a flow of air bubbles along the membrane surface for transporting the feed.
  • Said air bubbles are preferably of slug-type.
  • a larger flow (rate) of air bubbles is used compared to the first measuring step.
  • Said larger flow (rate) of air bubbles is preferably larger by at least 50%, more preferably by at least 75%, even more preferably by at least 100%.
  • the first cleaning step in said iteration is preferably carried out with differing conditions compared to the subsequent steps in said iteration.
  • the first cleaning step can be carried out during a longer period of time, such as at least 50% longer, preferably at least 75% longer and even more preferably at least 100% longer.
  • the trans membrane pressure (TMP) is held constant.
  • the rate of permeate is hence produced at constant TMP for each measuring step.
  • the iterative steps of cleaning and measuring are performed at least 10 times.
  • the first measuring step is performed until the rate of permeate has decreased to below a predetermined threshold.
  • the rate of permeate can be normalised by pressure and membrane area to yield a permeability.
  • the measuring step is performed for a predetermined period of time.
  • the cleaning steps comprise providing a flow of air bubbles along the membrane surface
  • the cleaning steps comprise a relaxation step.
  • said first parameter is related to a mechanical membrane cleaning action.
  • Mechanical membrane cleaning actions can refer to physical cleaning.
  • said mechanical membrane cleaning action is a back-wash.
  • Said mechanical membrane cleaning action can be a back-pulse.
  • Said mechanical membrane cleaning action is preferably aeration.
  • Said mechanical membrane cleaning action can be relaxation.
  • Mechanical membrane cleaning actions can refer to the dosing of a floe modifying agent. They can refer to the dosing of a coagulant. The floe modifying agent and the coagulant can be dosed as a preventive measure .
  • said second parameter is related to a chemical membrane cleaning action. More preferably, said chemical membrane cleaning action is maintenance chemical cleaning.
  • Chemical membrane cleaning actions can refer to the dosing of a floe modifying agent. They can refer to the dosing of a coagulant. The floe modifying agent and the coagulant can be dosed as a preventive measure.
  • methods of the invention comprise the step of using fuzzy set logic for calculating the value of said at least one first parameter.
  • Fuzzy set logic can be used for calculating the value of said at least one second parameter as well.
  • the reversible and the irreversible fouling propensity are multi-value indexes.
  • the multi-value indexes are obtained with the data collected in the first and iteratively performed measuring steps.
  • the first and iteratively performed measuring steps are repeated in order to monitor the evolution of the multi-value indexes with time.
  • a membrane filtration system comprising at least one membrane and a lower-level control system implementing a set of parameters arranged for actuating the cleaning actions of said at least one membrane.
  • the membrane filtration system further comprises a supervisory control system and a device for measuring a membrane fouling propensity of a feed applied to said at least one membrane.
  • the supervisory control system is preferably arranged for adjusting said set of parameters.
  • Each parameter of the set of parameters may control or govern a specific cleaning action .
  • the device for measuring is preferably coupled to the supervisory control system.
  • the device for measuring is preferably separate from the membranes of the membrane filtration system.
  • the supervisory control system and the device for measuring comprise means for carrying out the steps according to methods of the invention.
  • the supervisory control system comprises a first output arranged for setting one or more first parameters of said set of parameters.
  • the one or more first parameters are preferably related to mechanical (physical) cleaning.
  • the supervisory control system is arranged for calculating the value of said one or more first parameters based on the reversible fouling propensity.
  • the supervisory control system can comprise a second output arranged for setting one or more second parameters of said set of parameters.
  • the one or more second parameters are related to chemical cleaning. The value of said one or more second parameters is calculated based on the irreversible fouling propensity.
  • the device for measuring the membrane fouling propensity of a feed preferably comprises a first output arranged for providing information on the reversible fouling propensity of said feed and a second output arranged for providing information on the irreversible fouling propensity of said feed.
  • the first output of the device is preferably linked to the first input of the supervisory control system.
  • the second output of the device can be linked to the second input of the supervisory control system.
  • the membrane filtration system is pressure-driven. More preferably, said membrane filtration system is a membrane bioreactor.
  • the device for measuring the membrane fouling propensity of a feed comprises: a permeate production facility comprising a membrane, means for controlling and setting the trans-membrane-pressure across said membrane and means for measuring the permeate production rate through the membrane .
  • Figure 1 represents a scheme of the supervisory control of a membrane filtration plant.
  • Figure 2 represents an example of fuzzification of the temperature variable.
  • Three fuzzy sets (A, B, C) are defined and the membership functions of the temperature value to the fuzzy sets are plotted.
  • Figure 3 represents the scheme of figure 1 in which the supervisory control system is implemented based on fuzzy set logic.
  • Figure 4 represents schematically a device for measuring the reversible and irreversible fouling characteristics of a mixed liquor.
  • Figure 5 represents a graph of the measurements carried out with a device of figure 4.
  • the mass transfer coefficient (MTC) of the permeate also referred to as permeability, is determined over a time period and for each measurement step. Between each step a relaxation and aeration is carried out for removing the reversible fouling layer on the measurement membrane.
  • MTC mass transfer coefficient
  • Figure 6 plots the ratio of permeate volume to membrane area in function of the calculated ratio of hydraulic resistance due to reversible fouling to the hydraulic resistance of the membrane, based on the data of figure 5.
  • Figure 7 plots the ratio of permeate volume to membrane area in function of the calculated ratio of hydraulic resistance due to irreversible fouling to the hydraulic resistance of the membrane, based on the data of figure 5.
  • Figure 8 illustrates the evolution of the reversible fouling propensity with time for the mixed liquor of a membrane bioreactor being fed with municipal waste water, measured according to the invention.
  • Figure 9 illustrates the fuzzification of a reversible fouling fingerprint graph based on four normalised permeate volume on membrane area levels and five fuzzy sets.
  • Figure 10 illustrates the membership functions for the fuzzy sets applicable to the 50% level of figure 9.
  • a very important aspect of membrane fouling knowledge is the distinction between reversible and irreversible fouling.
  • the reversible fouling component is linked to the "loose” deposition of fouling constituents, possibly within the membrane pores but mostly on top of the membrane surface.
  • the deposited "layer” comprises a specific porosity which allows for the supernatant to be transported through that fouling layer and further through the membrane.
  • this deposited layer encompasses a hydraulic resistance of its own and causes an additional transport energy. Obviously, this energy waste should be minimized.
  • the reversible fouling layer is mechanically weak and can be disrupted through mechanical actions such as aeration (scouring of the membrane surface by air bubbles in order to remove fouling constituents deposited on the membrane surface) , back-washing, back-pulsing and relaxation.
  • aeration scoring of the membrane surface by air bubbles in order to remove fouling constituents deposited on the membrane surface
  • back-washing back-pulsing and relaxation.
  • the term “irreversible” fouling in the strict filtration sense would mean “irrecoverable” it is however used frequently in the literature and by researchers in the field to indicate the type of fouling which can be recovered by chemical cleaning.
  • the reversible fouling can be removed by mechanical actions.
  • the sticky type of fouling also referred to as the irreversible fouling, can not. Irreversible fouling can only be removed by the action of cleaning chemicals .
  • the increase of hydraulic resistance measured by such a dead-end device is hence related to the total fouling (sum of reversible and irreversible fouling) .
  • the present invention therefore provides a device that is able to monitor (to measure) both the reversible and the irreversible fouling propensity of a feed.
  • Such a measurement device opens the way for automating and optimizing the cleaning actions of a membrane filtration system (MFS) .
  • MFS membrane filtration system
  • Figure 4 shows schematically an embodiment of a measurement device of the present invention for measuring the fouling propensity of a feed (e.g. a feed to a MFS) .
  • the measurement device is based on a measurement membrane which is made to operate in cross-flow .
  • Figure 4 shows a scheme of the measurement device 40 with regard to a tubular membrane layout, but layouts for other types of membrane configurations are equally possible, such as for e.g. flat or capillary membranes .
  • Device 40 comprises a permeate production facility 42.
  • Permeate production facility 42 advantageously comprises an open-end tubular membrane 421 for carrying out an inside-to-outside filtration of the feed liquid 41.
  • the feed refers to a feed as applied at the surface of the membranes of a membrane filtration system.
  • the feed refers to the mixed liquor, or activated sludge, being a mixture of waste
  • feed liquid 41 is considered to be a sludge.
  • permeate production facility 42 is suspended in the liquid 41.
  • Such suspension can be obtained by providing a float 44 to which facility 42 is attached by fastening means 45 (such as e.g. strings or straps) .
  • Device 40 further comprises means 43 for producing the permeate at a specific TMP and to measure the corresponding permeate production rate. It is equally possible to maintain a specific permeate production rate and measure the corresponding TMP. However, in order to ensure that there is no influence of the compaction of the fouling layer due to a non-constant TMP, it is advantageous to keep the TMP constant during permeate production. The thus measured (calculated) decrease of membrane permeability can in the latter case be regarded as solely due to fouling and as not being influenced by compaction effects .
  • the TMP is preferably selected to ensure a high permeate flux. A high flux advantageously increases fouling rate and allows accurate measurements over even short time periods.
  • the TMP is preferably selected to be less than or equal to 1 bar, more preferably less than or equal to 0.5 bar and most preferably less than or equal to 0.2 bar.
  • means 43 comprise a vessel 431 for draining away the permeate from facility 42 and a permeate flow meter 432.
  • the permeate is drained from facility 42 by maintaining a subpressure (e.g. 1 bar or less) in vessel 431 by vacuum pump 433.
  • Pressure transducer 434 measures the trans- membrane-pressure (TMP) across membrane 421.
  • TMP trans- membrane-pressure
  • the TMP is hence caused by the subpressure in vessel 431, which causes a subpressure in a confined space 422 around the outside of the membrane 421.
  • the confined space 422 is delimited by the membrane 421 and facility 42 and is sealed such that permeate may enter only through the membrane 421.
  • device 40 comprises an aerator 426 at the bottom of membrane 421. Therefore, a compressor 435 produces pressurized air, which is fed to the aerator 426, at the bottom of membrane 421. Large air bubbles 423 are formed, which rise upwards in the tube 424 of the membrane 421. The air bubbles, while rising upwards, transport the sludge 41 upwards along the inner cavity (lumen) 424 of the tubular membrane. The rising air bubbles are of a slug shape and are very efficient in the transporting the sludge along the inner cavity 424. Due to the TMP, part of the sludge permeates through the membrane and generates a cross-flow through the membrane surface.
  • a mass flow controller 436 can further be provided in order to monitor and control the flow rate of air 423 fed to facility 42.
  • Device 40 preferably comprises a temperature sensor 425 for measuring the temperature of the sludge for calculating viscosity, which is needed for calculating a mass transfer coefficient (MTC) .
  • MTC mass transfer coefficient
  • the device of the invention preferably further comprises dedicated software for the data acquisition and data handling/calculation. Such a software may comprise proprietary MeFiAS® software by VITO, Belgium.
  • the measurement device 40 measures the fouling propensity of a feed (sludge) in cross-flow conditions and over longer periods of time (several hours or longer) .
  • the measurement device 40 is arranged to determine from the measured data both the reversible and the irreversible part of the fouling.
  • the method for measuring the total fouling propensity of the sludge comprises the steps of exerting a specified TMP across the membrane 421 and measuring the permeate production rate in function of time, over a chosen time period. According to the formula described in E. Brauns et al . cited in the prior art section, wherein:
  • V permeate volume (m 3 )
  • t time (s)
  • AP transmembrane pressure drop (Pa)
  • ⁇ absolute viscosity (kg/m.s)
  • R n membrane resistance (m "1 )
  • Rf all additional resistance from fouling (m "1 )
  • A membrane surface area (m 2 ) .
  • the fouling measurement is performed in a stepwise/cyclic manner as follows . [0070] In a first step, a low air flow rate inside the tubular membrane 421 is used.
  • the permeate production rate can be measured until the permeability of the membrane, or the permeate rate has decreased to below a predetermined threshold.
  • the permeability of the membrane is proportional to the inverse of the total hydraulic resistance (R m + Rf) of the membrane (and the fouling layer attached thereto) .
  • the permeate production rate can be measured until the permeability of the membrane has decreased to a value falling in the range between 10% and 50% of the initial value (i.e. of a clean membrane, with no fouling) , preferably to a value falling in the range between 20% and 50% of the initial value, more preferably to a value falling in the range between 20% and 40% of the initial value.
  • the first step can be preceded by a conditioning step.
  • the conditioning step the feed through the permeate production facility is stabilized, so as to obtain a homogeneous filling of the inner lumen of the tubular membrane 421 with feed liquid (sludge) . This can be achieved by a relatively high aeration (large flow of air bubbles) .
  • a cleaning step is carried out first, in which a higher air flow rate is used to remove the reversible layer while providing a relaxation at the same time (thus no permeate production) .
  • a relaxation comprises removing the TMP (no trans-membrane pressure gradient) . This removes the reversible fouling layer.
  • a measurement step according to the measurement procedure of the first step is repeated, either under same conditions or not.
  • the starting measurement data of the second and subsequent steps then corresponds to a permeability recovery.
  • the permeability that is not recovered is due to the remaining irreversible fouling part.
  • the TMP in the second and subsequent steps may differ from the TMP exerted in the first measurement step in cases wherein it is desired to keep the permeate flux constant. For reasons stated above, it is advantageous to keep the TMP constant.
  • the air (bubble) flow during the second and subsequent measurement steps can be different from the air bubble flow of the first step.
  • the air bubble flow rate in the second and subsequent measurement steps is higher than the air flow rate in the first step, with values of at least 50% higher (compared to the air flow rate of the first step) being preferred, values of at least 75% higher being more preferred and values of at least 100% higher being particularly preferred.
  • the air bubble flow rate of the cleaning steps and the measurement steps is preferably not the same.
  • the cleaning steps are preferably carried out with a higher aeration rate (air flow rate) .
  • the air flow rate during the cleaning step is preferably at least 10% higher and more preferably at least 20% higher than the air flow rate of the (second and subsequent) measurement steps.
  • Figure 5 shows a graph of consecutive measurements performed with a fouling measurement device of the invention. The graph plots different measurement data sets of permeate mass transfer coefficient (MTC) in function of time.
  • MTC permeate mass transfer coefficient
  • the mass transfer coefficient refers to a permeate rate normalised by the membrane area and TMP (units l/h.m 2 .bar) .
  • Set 51 refers to the first measurement step.
  • Set 52 refers to the second measurement step, after removal of the reversible fouling layer on the membrane 421.
  • the difference between the first measurement point 511 of the first step and the first measurement point 521 of the second step, namely an MTC difference of about 1600 l/h.m 2 .bar, is related to an irreversible fouling of the membrane 421. That irreversible fouling is subtracted from set 51 in order to calculate and extract the reversible fouling information. Indeed, it is assumed that the irreversible fouling between the last measurement of the first measurement step (5In) and the first measurement of the second measurement step (521) is the same.
  • FIG. 6 shows a reversible fouling curve and figure 7 shows an irreversible fouling curve.
  • the plots of figures 6 and 7 represent the ratio of permeate volume V to membrane area A versus the ratio of the hydraulic resistance due to respectively the reversible and the irreversible fouling to the membrane resistance.
  • the R f at each first sampling point (521) of a measurement step equals Rf rirr at that sampling point.
  • the assumption also implies that Rf,irr at each last sampling point (5In) of a measurement step equals Rf rirr at each first sampling point (521) of the subsequent measurement step.
  • Rf r r e v at each last sampling point can be calculated.
  • the values of Rf, re v and Rf, 1T r at each sampling point of a measurement step can be calculated by assuming a relationship between Rf, ir r and the permeate rate (or permeate volume) , such as a direct proportionality.
  • the entire multi-index values (i.e. the graphs of figs. 6 and 7) can change with time, e.g. due to a varying feed.
  • the measurement procedure as identified above is repeated in time to yield separate graphs (multi- index values) as in figs. 6 and 7 for each complete measurement procedure.
  • FIG. 8 This is illustrated in figure 8 for the reversible fouling propensity only.
  • the evolution of the reversible fouling propensity graphs for different days is plotted.
  • the data of fig. 8 was obtained by a measurement device 40, according to the invention, comprising a tubular membrane made of poly (vinylidene fluoride) (PVDF) having an inner diameter of 5.2 mm, a length of 680 mm and a nominal pore size of 0.03 ⁇ m.
  • the membranes used for the measurements all had a (normalised) clean water permeability (MTC) higher than 1000 1 m "2 h "1 bar "1 at a constant TMP of 0.1 bar.
  • MTC clean water permeability
  • the feed consisted of municipal wastewater, forming a mixed liquor, pre-screened at 0.75 mm.
  • the measurement protocol started with a conditioning step during which 100 ml min "1 of air is supplied at the bottom of the membrane tube, to ensure that the mixed liquor is homogenously distributed inside the membrane lumen when filtration starts.
  • a first measurement cycle was carried out, consisting of a filtration step (step IA) .
  • the filtration step was performed at a constant TMP of 0.10 bar and at an air flow rate of 40 ml min "1 , corresponding to a superficial gas velocity of 0.03 m s "1 .
  • Step IA continued until permeability had decreased to 30% of the initial permeability.
  • the following cycles each consisted of a physical cleaning step (relaxation step) , followed by a filtration (measurement) step.
  • the first cleaning step consisted of a 10 min relaxation at an air flow rate of 100 ml min "1 (specific aeration demand of 0.6 Nm 3 m ⁇ 2 h “1 ) .
  • Operational conditions for the subsequent filtration steps were a constant TMP of 0.10 bar, an air flow rate of 80 ml min "1 (superficial gas velocity of 0.07 m s "1 ) and a duration of 5 min. Removal of the remaining reversible fouling during the second and subsequent cleaning steps was achieved through a 3 min relaxation step at an air flow of 100 ml min "1 . At least 10 cycles were applied to ensure an adequate measurement of the irreversible fouling propensity.
  • the reversible and irreversible fouling propensity measured (and calculated) by the measurement device of the invention may be represented as curves and thus need not be a single point value.
  • the fouling measurement device of the invention thus allows to measure both the reversible and irreversible fouling propensity of the sludge to induce membrane fouling. At the end of an entire measurement cycle, e.g.
  • the membrane 421 of facility 42 is not useful anymore for further measurements. It is fouled too much.
  • the membrane 421 should be replaced by a new or clean membrane.
  • the removed membrane may be disposed of or may be cleaned in order to remove the irreversible fouling layer.
  • facility 42 of measurement device 40 may be provided with a membrane loader (not shown in figure 4) .
  • the membrane loader loads a clean membrane at the beginning of a new cycle of measurements and removes the fouled one.
  • the membrane loader is arranged to keep a stock of several clean membranes.
  • the loader then may put the fouled membranes in a stack such that at defined time intervals they may be collected for cleaning or disposal.
  • the loader then may be loaded with a new batch of clean membranes. More preferably, the loader is provided with a facility to chemically clean the membranes.
  • the measurement device 40 is able to continuously monitor the fouling propensity of the sludge.
  • the measurement device produces an output evaluating the reversible and irreversible fouling characteristics of the sludge.
  • the present invention now discloses a system for optimizing and automating the control of the cleaning actions of a membrane filtration system (MFS) .
  • MFS membrane filtration system
  • Such a system calculates the parameters relating to the cleaning actions on the membranes (e.g. time interval for cleaning, duration, etc.) in function of the quality of the feed (reversible and irreversible fouling characteristics) . This leads to a more efficient operation of the membrane filtration system.
  • the invention provides a supervisory control system (SCS) and a method of supervisory control, which supersedes the lower-level control system of an MFS, the latter control system being known in the art.
  • SCS supervisory control system
  • FIG 1 shows this schematically.
  • a membrane filtration system 10 is controlled by a lower- level control system 11, which may be a PLC-based control or a MeFiAS® control system (which is proprietary control software/hardware of VITO, Belgium) for controlling e.g. the actuators for the cleaning actions (e.g. the mechanical and/or chemical cleaning) .
  • the lower-level control system 11 is implemented with set-point parameters 12, relating to the cleaning actions.
  • the parameters 12 may refer to time intervals, dosing of chemicals, etc. and will be discussed more into detail later on.
  • the parameter values are fine-tuned when the MFS is installed, and may be adjusted occasionally later on.
  • a supervisory control system 13 is arranged to continuously
  • a primary input data is information on the reversible and irreversible fouling of the membranes and/or information on the reversible and irreversible fouling propensity of the feed. Therefore, the supervisory control system comprises a first input 141 for gaining information on the reversible fouling (of the feed or of the membranes themselves) and a second input 142 for gaining information on the irreversible fouling (of the feed or of the membranes themselves) .
  • the reversible and irreversible fouling information is measured by one or more measurement devices 15.
  • the measurements of a fouling sensor are thus always primary inputs 141 and 142 of the SCS.
  • the primary reversible and irreversible fouling information may be complemented by other measurement data, such as the EPS concentration (extracellular polymeric substances) , feed temperature, dissolved oxygen, pH, biomass concentration (MLSS), etc.
  • This data is provided by measurement devices 16 and is made available to the supervisory control system at one or more inputs 17. It is important to note that for specific additional data adequate sensors and measuring devices (methods) are needed.
  • the measurement device 15 may perform its measurements on a part of the MFS 10 itself, or on a sample 19 withdrawn from the MFS (e.g. part of the feed withdrawn before it enters the MFS) and fed to the fouling sensor 15.
  • the measurement device 15 is a device which is separate and distinct from the MFS 10.
  • the measurement device 15 is arranged to receive a feed, which is at least a sample of the feed applied to the membranes of the MFS 10.
  • a second set of parameters 12 related to chemical cleaning actions may be controlled based on information available at input 142
  • Such a supervisory control system enables to optimise the operation of membrane filtration plants (optimized membrane surface, less aeration, less mechanical and chemical constraints on the membranes, etc.) .
  • the cleaning actions in a membrane filtration system can be grouped into two types, viz. the mechanical and chemical cleaning actions, which counter two specific types of fouling, respectively the reversible fouling and the irreversible fouling.
  • the supervisory control system is provided with inputs 141 and 142, each input relating to only one of the two cleaning types. This allows to achieve an improved optimization of the cleaning actions and a more efficient operation of the MFS.
  • the input 141 gives information on the reversible fouling component of the total fouling and hence allows for the control of the mechanical membrane cleaning oriented actions.
  • the input 142 gives information on the irreversible fouling component and allows for the control of the chemical membrane cleaning actions.
  • the information supplied at inputs 141 and 142 may be provided by a measurement device 40.
  • Two main control groups can be considered within the control actions of a supervisory control system of a membrane filtration plant.
  • a first group is related to the reversible fouling and therefore to the related mechanical cleaning controls or to a reversible fouling reduction strategy.
  • a second group is related to the irreversible membrane fouling effects, which can not be removed by the mechanical actions as used for reversible fouling but only by chemically cleaning the membrane.
  • the reversible membrane fouling control can be tackled in different ways.
  • the reversible fouling component is linked to the "loose" deposition (e.g. weak Van der Waals forces) of fouling constituents, possibly within the membrane pores but mostly on top of the membrane surface.
  • the deposited "layer” comprises a specific porosity which allows for the supernatant to be transported through that fouling layer and further through the membrane.
  • this deposited layer encompasses a hydraulic resistance of its own and therefore such layer causes an additional transport energy (pumping energy) .
  • this energy waste should be minimized in an MFS and therefore also the hydraulic resistance according to this layer.
  • the reversible fouling resistance thus should be minimized.
  • the reversible fouling layer behaviour may be quite complex as a result of the complicated composition of the bioreactor sludge which consists of floes (bacteria) and suspended solids.
  • the reversible fouling layer is mechanically weak it is possible to exercise a specific "mechanical” action on the layer in order to disrupt it or to make it as thin as possible.
  • TMP trans-membrane-pressure
  • a sustained pressure gradient can cause a compression of the reversible fouling layer which increases the hydraulic resistance of the fouling layer.
  • relaxation A temporary removal of the pressure gradient (called relaxation) thus can be beneficial, in a way that the unwanted compression can be countered.
  • the fouling layer is restored to a more loosely bounded system which then can be removed more easily by a parallel/succeeding mechanical action or preventive action
  • a back-wash is often used in pressure driven membrane filtration in order to remove regularly the reversible fouling layer on top of the membrane surface.
  • a back-wash action comprises sending back a specific amount of permeate through the membrane to flush away the non- sticking fouling layer. This action should be fine-tuned in order to spill only a minimum of permeate and to minimize the interruption time of permeate production.
  • Possible set- point parameters related to the back-wash action are the:
  • back-wash flux a high flux can be beneficial for extensive and rapid membrane cleaning
  • - back-wash duration an efficient backwash needs a minimum of back-washing time
  • back-wash interval a shorter interval time between two back-wash actions is needed with a higher reversible fouling potential of the sludge.
  • a back-pulse is in fact a high amplitude, very short duration type of back-wash.
  • the shock-wave-resembling back-pulse can be very efficient with respect to an improved all-membrane-surface-area cleaning. Since the membrane reversible fouling layer is not necessarily homogeneous over the complete membrane surface area, it is possible that during a common back-wash action the permeate will flow through the lower hydraulic resistance zones but not through the somewhat higher hydraulic resistance zones.
  • a common back-wash could be of a lower efficiency when compared with the shock-wave type of back-pulse action.
  • Possible set-point parameters related to the back- pulse action are the: - back-pulse amplitude: a higher amplitude means a higher exerted cleaning energy,
  • — back-pulse duration a longer pulse increases the removed quantity of the reversible fouling layer and the — back-pulse interval: a shorter time interval between two back-pulse actions is needed with a higher reversible fouling potential of the sludge.
  • aeration interval in the case of a continuous aeration, the aeration interval is not interrupted, but in the case of an intermittent aeration, a shorter interval is needed with a higher reversible fouling potential of the sludge; a burst type of aeration (temporarily burst) could have an efficient mechanical cleaning effect in some cases.
  • a modulated filtration mode may be used in membrane filtration, and membrane bioreactor filtration in particular. Permeate is produced during a specific filtration interval, being followed by a relaxation interval, in which permeate is not produced. During the relaxation interval the TMP gradient becomes zero. This allows for the fouling layer to get less compacted during the relaxation interval and therefore allows to be removed more easily by mechanical action (aeration, backwash, etc.).
  • Possible set-point parameters related to the aeration action are the: - relaxation duration: an increased relaxation period simplifies the removal of the reversible fouling layer and the - relaxation interval: a shorter relaxation interval is needed with a higher reversible fouling potential of the sludge .
  • a suitable sludge floc-modifying agent is found to be effective with respect to the reduction of the reversible fouling tendency.
  • the floc- modifying agent causes the creation of a floe population with a higher permeability than in normal circumstances on the membrane surface, or possibly with a lower mechanical compaction sensitivity. In these cases, the dosing of such an agent could be considered.
  • floc- modifying agent works primarily on the reversible fouling layer, it may be considered as an additional type of mechanical cleaning action, or at least as an action in support of the mechanical cleaning.
  • Possible set-point parameters related to the dosing of floc-modifying agent could be defined as: — floc-modifying agent dose and the
  • a second important fouling factor is the irreversible fouling.
  • This "sticking" type of fouling can not be removed by the mechanical actions for removing the reversible fouling layer described above.
  • the irreversible type of membrane fouling can only be countered by chemically cleaning the membrane surface.
  • the chemical cleaning can restore part of the original permeability of the membrane but not the irrecoverable part.
  • a second control group may be comprised in the supervisory control system, which is related to the control of the chemical cleaning actions.
  • two types of chemical cleaning are used: a regular maintenance chemical cleaning (MC) and an intensive chemical cleaning (IC) .
  • An IC is only done a few times (or even once) a year and therefore may or may not need to be incorporated in the supervisory control actions, since it is done in a pragmatic way, based on experience.
  • the MC however is determined by the irreversible fouling propensity of the sludge. Possible set-point parameters related to the MC are the:
  • a preventive action may be an alternative option in order to avoid - completely or partly - the occurrence of irreversible fouling. This can be done by using specific coagulants which envisage to neutralize the irreversible fouling constituents in the sludge
  • membrane fouling consists of very complex phenomena which in most cases can not be described adequately by mathematical models. There are numerous fouling constituents which act in parallel. These fouling constituents interact with the membrane surface and membrane pores in very complex ways. Therefore, a universally applicable mathematical fouling model which allows to accurately predict the fouling behaviour of a membrane is very difficult to implement.
  • the solution to the modelling problem of the fouling adopted in the present invention therefore is to implement in the supervisory control system a set of control rules (mathematical, fuzzy, etc.) which mimic to a certain extent a human operator who uses heuristic knowledge in order to control the cleaning actions of a membrane filtration plant in an acceptable way.
  • This heuristic knowledge is largely based on membrane fouling knowledge and in particular on reversible and irreversible membrane fouling knowledge.
  • the reversible and irreversible fouling knowledge is obtained, according to the present invention, by way of measurement procedures as identified above.
  • the knowledge is advantageously expressed as a hydraulic resistance (normalised) related to the reversible or the irreversible fouling component of a feed.
  • Those hydraulic resistances can be obtained for various permeate volumes (normalised) as multi-value indexes. The indexes can be monitored at regular intervals in time.
  • the supervisory control system can be implemented with control rules based on classical mathematical regression analysis of the above multi-value indexes. In the case of regression analysis, the multi- value indexes (graphs) can be represented by an adequate mathematical equation. Another approach, according to the invention, is to implement the control rules based fuzzy set logic. In the latter, the multi-index values can be converted into fuzzy sets, the values of which trigger actions of the supervisory control system according to the implemented control rules. [0117] An embodiment of a supervisory control system and method implemented with fuzzy set logic is outlined in what follows.
  • the calculations and control actions taken within the supervisory control system 13 may be performed based on fuzzy set logic (FSL) .
  • FSL fuzzy set logic
  • the value of a variable - e.g. temperature - is accorded one or more fuzzy sets - e.g. low, medium and high.
  • the strength of FSL lies in the fact that the borders delimiting the fuzzy sets need not be crisp.
  • a temperature value of 20 0 C may belong both to the set "low” and to the set "medium”, i.e. the temperature value of 20 0 C has a membership of both the set "low” and the set "medium”.
  • FIG 2 This is shown in figure 2, where the membership functions of temperature values are drawn for three fuzzy sets: A (low in the previous example), B (medium) and C (high) .
  • the temperature value of 20 0 C has a membership of 0.5 for set "low” and 0.5 for set "medium”.
  • control rules may be implemented, based on the fuzzy sets, which allow for actions to be undertaken.
  • the implementation of fuzzy set logic in a supervisory control system of the invention may be implemented as shown in figure 3.
  • the SCS 13 comprises a control block 131, 132, 133, etc. respectively for each set-point parameter 121, 122, 123, etc. from the set 12.
  • Each control block comprises a fuzzification module 30, a fuzzy inference module 31, a fuzzy rule module 32 and a defuzzification module 33.
  • the role of each of these modules is outlined in what follows.
  • the fuzzification module 30 translates the measured values of one or more inputs to the SCS (reversible and irreversible fouling and additional input parameters) into linguistic variables, linked to predefined fuzzy sets. Each input is linked to a linguistic variable.
  • the linguistic input variables "F rev ", "F irr " and "Temp” could be defined. In this way all possible relevant input parameters in the supervisory control can be defined as linguistic variables. For all these linguistic variables the according fuzzy sets need to be defined.
  • a fuzzification is preferably performed based on the multi- value index (or the graph) as a whole.
  • the latter whole content approach can be obtained by using a fuzzy image recognition method, as is explained further for only the reversible fouling fingerprint index (graph) .
  • the method is completely analogous for the irreversible fouling fingerprint.
  • a fuzzy control block embodies a fuzzification module, an interference module, a fuzzy rules module and a defuzzification module as set out above.
  • Such set-up can also be used in an image recognition environment to evaluate a multi-value index as a whole, or when the multi-value index is represented as a graph, the "shape" or position of a graph. Since the reversible and irreversible fouling fingerprint graphs, e.g. those in figs.
  • a theoretically horizontal fouling graph indicates the worst possible situation, since the system can produce no permeate at all: the hydraulic resistance increases immediately to a very high value, thus 100% fouling propensity of the mixed liquor. All real-case graphs thus will be located between the two extremes.
  • a normalized V/A ordinate axis a minimum level of 0% and a maximum level of 100 % (the level of V/A normalised to 100 % could e.g. be linked to a fixed level of 0.020 m 3 /m 2 ) .
  • VL Very Low
  • L Low
  • M Medium
  • H High
  • VH Very High
  • these can be selected at respectively 12.5 %, 25 %, 50 % and 100 %.
  • at each level distinct VL, L, M, H and VH fouling zones can be identified.
  • curve typically crosses the four levels 12.5 %, 25 %, 50
  • VA12.5, VA25, VA50 and VAlOO respectively can be used as input variables to a fuzzy control block.
  • fuzzy IF THEN rules can be set up for possible combinations of the VL, L, M, H and VH fouling zones at the four levels 12.5 %, 25 %, 50 % and 100 %. A number of these rules are given in table 3.
  • the linguistic variables from the fuzzification module 30 are processed in the inference module 31.
  • the inference module 31 uses the FSL conditional rules of the fuzzy rules module 32, which are constructed from expert knowledge of e.g. a human operator of a membrane filtration plant.
  • the fuzzy rules comprise the fuzzified values of one or more of the inputs 141, 142 and 17 and combine those through fuzzy inference into a linguistic fuzzy output variable.
  • Each linguistic fuzzy output variable is linked to a set-point parameter 121, 122, 123, etc.
  • a set of fuzzy rules within the fuzzy rules module 32 comprises also a multitude of fuzzy IF... THEN rules. Moreover, multiple input variables may be processed by such fuzzy rules as fuzzy operators AND, OR, etc. can be integrated.
  • fuzzy inference handling of the fuzzy rules two major actions are executed. First the IF parts of the rules are calculated (which is called aggregation) whereafter the THEN parts of the rules are calculated (which is called composition) . The calculations result in a linguistic value of the output variable (parameter) .
  • the classic fuzzy operators AND, OR, etc. are not related in any way to the classic Boolean logical operators AND, OR, etc. The classic Boolean operators in effect can not handle conditions which are "more-or-less" true. Therefore specific fuzzy operators such as AND and OR have been defined mathematically in fuzzy set handling.
  • Each set-point parameter' s linguistic value is subsequently translated into a real, physical (crisp) value by the defuzzification module 33. This value is needed to actually adjust the value of the set-point parameter (e.g. 121) of the lower-level classic control system.
  • each Fuzzy Set Logic control block 131 can be needed for each set-point parameter of the lower- level MFS-control.
  • each Fuzzy Set Logic control block 131, 132, 133, etc. shows the same features but each block is tuned to the specific set- point parameter linked to that block.
  • Different defuzzification methods can be deployed in FSL control but often the Centre-of-Gravity method is used. Such methods result in a crisp output parameter value which is even not discontinuous with changing input parameter values. Such defuzzification clearly relates to the human operator mimicking property of a fuzzy control approach.
  • An EPS concentration sensor may provide an input 17 to a supervisory control system 13 and is preferably used for the control of dosing coagulants in order to prevent (anticipate) membrane fouling, instead of remedying an already occurred irreversible membrane fouling by chemical cleaning (MC) .
  • MC chemical cleaning
  • Heuristic knowledge about the effect of the EPS concentration value on the dosing of coagulants can be implemented in a specific control block of the type 131.
  • Table 1 gives an overview of the set-point parameters discussed above and related to the mechanical and chemical cleaning actions.
  • each set-point parameter of table 1 would imply a separate control block of the type 131.
  • the SCS 13 of the invention may restrict its supervisory control to only a subset of the set-point parameters listed in table 1. Additional set-point parameters may equally be identified and supervisory controlled.
  • a fouling sensor such as the fouling measurement device of the invention is used in this example to measure the reversible fouling propensity of the mixed liquor and thus produces the main input parameter value of the supervisory control system 13, namely a reversible fouling parameter.
  • temperature is also considered in this example as an SCS input parameter. Additional input parameters may be introduced as well but in this example, the number of input parameters is confined to two, for simplification reasons. For the same reasons, in this example, only AirBubFlow as an output variable is discussed.
  • the linguistic name for the reversible fouling input variable is "Frev" and for the mixed liquor temperature the linguistic name is "Temp".
  • a membership of Frev to its fuzzy sets can be implemented by fuzzifying the curve of figure 6 as a whole. This can be done by choosing multiple R to t,rev/R m x-axis values and impose on each of these the specified fuzzy sets.
  • Table 3 Fuz zy inference rules for the revers ible foul ing propens ity f ingerprint .

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Abstract

L'invention concerne un procédé de commande d'actions de nettoyage de membrane d'un système de filtration sur membrane. Ce procédé consiste à mesurer le taux de perméat produit par une installation de production de perméat comprenant une membrane, en fonction du temps, au cours d'une première étape de mesure ; à réaliser à plusieurs reprises les étapes de nettoyage de la membrane de ladite installation, par au moins une action de nettoyage mécanique ; puis à mesurer le taux de perméat produit par l'installation en fonction du temps. Le procédé selon l'invention consiste également : à calculer une propension d'encrassement réversible de la charge en fonction du taux de perméat qui est récupéré après chaque étape de nettoyage ; à calculer une propension d'encrassement irréversible de la charge en fonction du taux de perméat qui n'est pas récupéré après chaque étape de nettoyage ; et à calculer la valeur d'au moins un premier paramètre associé à une action de nettoyage mécanique de la membrane en fonction de la propension d'encrassement réversible. Le procédé selon l'invention peut également consister à calculer la valeur d'au moins un deuxième paramètre associé à une action de nettoyage chimique de la membrane en fonction de la propension d'encrassement irréversible. L'invention concerne également un système de filtration sur membrane comprenant un système de commande de surveillance mettant en œuvre ce procédé.
PCT/EP2008/055113 2007-04-27 2008-04-25 Systeme et procede de commande de surveillance pour nettoyage de membrane WO2008132186A1 (fr)

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WO2010015543A1 (fr) * 2008-08-06 2010-02-11 Otv Sa Installation et procede de traitement d'eau optimise
WO2010109265A1 (fr) * 2009-03-27 2010-09-30 Abb Research Ltd Procédé et système pour une optimisation en ligne d'un processus de filtration sur membrane
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EP2626126A1 (fr) * 2012-02-13 2013-08-14 Krones AG Procédé de commande et/ou de réglage d'installations de filtrage pour l'ultrafiltration
WO2014025194A1 (fr) * 2012-08-09 2014-02-13 Cheil Industries Inc. Dispositif d'aérateur, système de filtre et procédé d'aération d'un filtre
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WO2014198475A1 (fr) * 2013-06-14 2014-12-18 Abb Ag Procede de prevision d'instant de nettoyage de membrane et systeme associe
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WO2016181000A1 (fr) * 2015-05-11 2016-11-17 Acciona Agua, S.A.U. Dispositif de détection de l'encrassement de membranes
ES2589479A1 (es) * 2015-05-11 2016-11-14 Acciona Agua, S.A.U. Dispositivo para la detección del ensuciamiento de membranas
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