EP2356080A1 - Dispositif et procede de traitement des eaux impliquant une filtration a travers au moins une membrane immergee - Google Patents
Dispositif et procede de traitement des eaux impliquant une filtration a travers au moins une membrane immergeeInfo
- Publication number
- EP2356080A1 EP2356080A1 EP09768155A EP09768155A EP2356080A1 EP 2356080 A1 EP2356080 A1 EP 2356080A1 EP 09768155 A EP09768155 A EP 09768155A EP 09768155 A EP09768155 A EP 09768155A EP 2356080 A1 EP2356080 A1 EP 2356080A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- membrane
- particles
- activated sludge
- volume
- treatment
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Withdrawn
Links
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
- C02F3/02—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
-
- 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
- C02F3/08—Aerobic processes using moving contact bodies
- C02F3/085—Fluidized beds
-
- 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
- C02F2303/20—Prevention of biofouling
-
- 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 relates to a water treatment method and an associated device.
- Activated sludge eliminates carbon, nitrogen and phosphorus pollution.
- the membrane flat or organic hollow fiber
- the liquids before filtration may have a concentration of the order of 10 g / l of suspended matter.
- the membranes ensure the separation between activated sludge and purified water.
- the effluents after treatment are sucked or evacuated by gravity.
- the clogging can in part be controlled by applying to the device backwashing phases, where the water circulates against the current.
- a specific aeration device is also used to reduce the clogging, in stationary mode. Such an aeration device is highly energy consuming, which is a major drawback.
- Document JP 63-214177 discloses a water treatment system operating with a membrane bio-reactor, the membranes being integrated into the activated sludge tank, into which particles of less or equal hardness are introduced. to that of the separation membrane.
- the particles have a density greater than 1, and are between 1 and 2 mm in diameter.
- the volume occupied by the particles is 10 to 50% of the volume of the membrane tank.
- the particles are resin, gel or polyvinyl alcohol gum, or in some cases ceramic or granular activated carbon. They are displaced or suspended by a flow of liquid and gas in the membrane tank, with a speed of 1 to a few meters. s "1. In one case, the particles are suspended in a fluidized bed.
- a solution is therefore sought to reduce the energy consumption of existing devices, and more specifically to reduce clogging in operation without having to provide an air supply to the membranes.
- the solution must also preserve the life of the membranes, avoiding any inadvertent damage.
- the present invention proposes a method of treating a water to be treated involving filtration through at least one membrane coupled to an activated sludge reactor, characterized in that added particles are present in at least one volume of activated sludge in contact with the membrane and in that variations of a flow rate generated in said volume of activated sludge parallel to the membrane are applied thanks to which it is created in the immediate vicinity of the membrane a medium turbulent intensity level higher than that corresponding to a constant flow. It is specified that added particles are understood to mean particles which are not present initially in the water to be treated.
- the flow variations are applied so as to create an alternation of turbulent intensity levels, or a mean turbulent intensity level higher than that corresponding to a constant flow rate.
- the variations of a flow rate comprise the alternation of at least a first so-called “low flow” rate phase and a "high speed” second flow rate phase.
- the rate variations include an alternation of at least a first and a second phase, the first phase rate corresponding to an average tangential velocity of between 0.01 and 0.1 ms -1 applied for a period of time between 0 and 600 s, preferably between 10 and 45 s.
- the flow corresponds to an average tangential velocity of between 0.1 and 0.35 ms -1. applied for a period of between 0 and 3600 s, preferably between 25 and 600 s.
- the duration of the first phase be between 0.75 and 1.25 times the duration of the second phase.
- the ratio between the high bit rate and the low bit rate is between 1.5 and 12, and preferably between 2 and 3.5.
- the particles are set in motion in a fluidized bed. This advantageously saves energy compared to a device using an aeration system.
- the membrane is confined so as to channel the overall movement of said volume of activated sludge. This advantageously makes it possible to minimize the energy required for generating the flow rate.
- the flow variations are generated by regulating a recirculation flow control device.
- certain particles have a density between 1 and 10, preferably between 1.5 and 3, and some particles have a form factor of between 1 and 20, preferably between 1 and 7. It is particularly preferred that certain particles essentially comprise an organic, inorganic or composite material, and in a very particularly advantageous embodiment, the particles are glass beads.
- the glass beads used with tangential speeds as presented above, have the advantage of maintaining the integrity of the surface of the membranes.
- At least some particles have a diameter of between 0.05 and 0.6 times the diameter of a liquid vein. It is specified that the notion of liquid vein diameter here means the smallest distance between two walls of the liquid vein.
- the volume filling rate of the membrane vessel by the particles is between 0.5 and 50%, and preferably between 20 and 40%.
- at least one membrane is a plane membrane.
- at least one membrane is a hollow fiber membrane.
- At least one membrane is placed vertically or substantially vertically.
- At least one membrane is in a compartment integrated in the biological reactor.
- at least one membrane is in a specific compartment out of the biological reactor.
- a method of treating a water to be treated involving filtration through at least one membrane coupled to an activated sludge reactor and whose permeability is maintained over time, characterized in that added particles are present in at least one volume of activated sludge in contact with the membrane and in that variations of a flow rate generated in said volume of activated sludge parallel to the membrane are applied to the particles.
- a device for treating a water to be treated comprising at least one filtration membrane coupled to an activated sludge reactor and whose permeability is maintained over time, characterized in that it comprises means for applying to added particles present in at least one volume of activated sludge in contact with the membrane of variations of a flow rate generated in said volume of activated sludge parallel to the membrane.
- the variations of a flow rate are applied so as to create in the immediate vicinity of the membrane a mean turbulent intensity level higher than that corresponding to a constant flow rate.
- a treatment device for a water to be treated comprising at least one filtration membrane coupled to a reactor to be treated.
- activated sludge characterized in that it comprises means of application to added particles present in at least one volume of activated sludge in contact with the membrane of variations of a flow rate generated in said volume of activated sludge parallel to the membrane , whereby the variations of a flow rate are applied so as to create in the immediate vicinity of the membrane a mean turbulent intensity level higher than that corresponding to a constant flow rate.
- Figure 1 is a diagram of a first embodiment of a device according to the invention.
- Figure 2 is a detail view of the device of the previous figure, a first phase of operation.
- Figure 3 is a view similar to that of Figure 2 of the same device, during a second phase of operation.
- Figure 4 is a set of permeability curves measured experimentally under different conditions with the device of the first embodiment.
- Figure 5 is also a set of permeability curves measured experimentally under different conditions with the device of the first embodiment, on a longer time scale.
- Figure 6 is a diagram of a second embodiment of a device according to the invention.
- Figure 7 is a diagram of a third embodiment of a device according to the invention.
- a biological reactor 5 is coupled to a system of two membranes 6 in a manner known per se, the membranes being confined in a tank called membrane tank 11.
- the number of membranes depends on the implementation of the invention. Typically, 5 membranes can be used.
- the raw water to be treated is introduced into the biological reactor
- the biological reactor also has a ventilation system 4 at the bottom and an escape route for excess biological sludge 3, also at the bottom. It is specified that, alternatively, the reactor 5 could comprise several compartments, some being ventilated and others not.
- the membranes 6 are here flat and vertical membranes of width 0.515 m and height 1.47 m.
- the filtration area of each of the two membranes is 1.37 m 2 .
- the distance between two membranes is 7 mm.
- a pump 12 controlled by a controller 8 and a particle introduction path 10 are installed on the access path 13 of the biological reactor 5 to the membrane vessel 11.
- This access path 13 connects the lower part of the biological reactor 5. at the lower part of the membrane tank 11.
- the pump 12 operates with a flow rate of 6 m 3 / h during a first phase, then 12 m 3 / h during a second phase, the controller 8 ensuring the alternation of the two phases .
- the pumped sludge is mixed with particles 7 in the membrane tank 11, the particles 7 being present in a proportion of between 3 and 30% of the useful volume of the membrane tank, depending on the implementations.
- the particles 7 are here glass balls of form factor 1,
- a collector 9 is installed on the recirculation channel 14 of the membrane tank 7 to the biological reactor 5, which connects the upper part of the membrane tank 7 to the upper part of the biological reactor 5.
- the collector 9 serves as a separation system for the particles and biological sludge.
- this collector 9 is installed on the upper part of the membrane tank, at the entrance of the recirculation channel.
- the membrane tank 11 has a confinement favorable to the unclogging of the membranes 6. It includes a complete confinement of the liquid vein delimited by the membrane with a minimization of the dead volume.
- the effective volume of the membrane tank is 200 L.
- FIG. 2 presented a front view of a membrane 6 in the membrane tank 11.
- the gateway 13 of the bioreactor 5 to the membrane tank 11 injects an activated sludge taken from flow Q m ⁇ n the biological reactor 5, from the bottom of the membrane tank 11 upwards.
- the particles 7 are confronted with a flow of liquid and mud from bottom to top and follow various movements in the liquid, near and in contact with the membrane 6.
- FIG. 2 shows an equilibrium configuration, where the set formed by all the particles is generally stable, some particles having an upward movement, others downward.
- the upper part of the membrane tank 11 opens on a collector 9, which is in this embodiment, a zone of tranquilization caused by a sudden enlargement of the tank.
- the excess liquid flows via the collector 9 and joins the recirculation channel 14 shown in FIG.
- FIG. 3 there is shown a same front view of the membrane vessel.
- the injected flow rate is this time greater than Q m ⁇ n, and reaches a value Q ma ⁇ , which in the embodiment shown is equal to twice the value of CWi
- the particles 7 are present in all the height of the tank membrane, because of the flow rate which is sufficient to bring one or more particles to the top of the tank.
- the flow rate Q max applied in the configuration of FIG. 3 is nevertheless sufficiently small so that the particles are approximately uniformly distributed over the entire height of the membrane tank, the gravity being sufficient to lower some down the tank. .
- FIG. 4 there is shown the evolution of permeability measurements of the membrane system as a function of time over a period of 4 hours from the start of operation of the system, in three different operating modes.
- the measurements are carried out at 20 ° C., and the permeability values are relative to the m 2 of membrane.
- the device of FIG. 1 is equipped with five membranes of width 0.515 m confined laterally, the membrane tank 7 having a total liquid vein of
- the device of FIG. 1 operates without particles and without aeration at the level of the membranes. It is found that the permeability, initially close to 2000 L / hm 2 .bar decreases rapidly to reach a value of about 100 L / hm 2 .bar after one hour of operation. The permeability then remains close to this latter value, referred to as the near-frontal level of filtration.
- reference numeral 2 the evolution observed with aeration according to the prior art was shown, with a flow rate of 0.6 Nm 3 of air (Normo cubic meter of air) per m 2 of membrane, according to the prior art. The permeability starts at a value close to 1000 L / hm 2 .bar and then evolves around the value of 800 L / hm 2 .bar, about 7 times higher than the level of near-frontal filtration.
- FIG. 5 shows the evolution of the permeability of the membrane over longer periods of up to 70 hours. Two implementation regimes are represented.
- reference numeral 1 there is shown a test with a filling rate of the particles of 3% of the volume of the membrane tank and a flow rate of 6m 3 / h during a phase of 30 s, followed by a flow rate of 12 m 3 / h during a phase of
- the permeability decreases to a value of 600 L / hm 2 .bar, or about 6 times the value of quasi-frontal permeability.
- the turbulent intensity at the membrane is 17%.
- reference numeral 2 there is shown a test with a filling rate of the membrane tank by glass beads at 30% of the volume, and an alternation of a phase of 30 seconds of flow at 6 m 3 / h corresponding at a tangential velocity of 0.08 m. s "1 with a phase of 30 seconds flow at 12 m 3 / h corresponding to a tangential velocity of 0.15 m. s " 1 .
- the permeability is maintained at a value of 1100 L / hm 2 .bar, evening 11 times more than the value of quasi-frontal permeability.
- the turbulent intensity of the membrane, averaged over a dozen cycles, is 42%.
- a biological reactor 50 is coupled to a system of two membranes 60 in a manner known per se, the membranes being confined in a tank called membrane tank 110.
- the raw water to be treated is introduced into the biological reactor 50 via an upstream inlet 10 in the upper part of the tank 50.
- the treated water leaves the filtration tank via a downstream outlet 20 in the upper part of the membrane tank 110.
- the biological reactor also has a ventilation system 40 at the bottom and an escape route biological sludge in excess 30, also at the bottom.
- a pump 120 is installed on the access path 130 of the biological reactor 50 to the membrane tank 110.
- This access path 130 connects the lower part of the biological reactor 5 to the lower part of the membrane tank 11.
- the pump has a continuous regime, unlike that used in the first embodiment. Downstream of the pump 120 is installed a by-pass system, making it possible to direct part of the flow generated by the pump 120 out of the access path 130, towards a clearance path 150 bringing the surplus liquid to the reactor Biological 5, in the upper part of it.
- a particle introduction path 100 is installed on the access path 130.
- the pumped liquid is thus mixed with particles 70 in the membrane vessel 110.
- a gate 80 is installed on the recirculation channel 140 of the membrane tank to the biological reactor, which connects the upper part of the membrane tank to the upper part of the biological reservoir.
- the gate 80 has a mesh size smaller than the minimum diameter of the particles, for example equal to 0.8 times the diameter of the particles.
- This gate 80 serves as a separation system particles and biological sludge, the particles being brought back by gravity to the membrane tank 110.
- FIG. 7 another embodiment is shown. It includes the use of a filtration tank integrated in the biological sludge tank.
- a biological reactor 51 is coupled to a system of two membranes 61 in a manner known per se, the membranes being confined in a tank called membrane tank 111 integrated in the biological reactor 51.
- the raw water to be treated is introduced into the biological reactor 51 via an upstream inlet 11 in the upper part of the tank 51.
- the treated water leaves the filtration tank via a downstream outlet 21 in the upper part of the membrane tank 111.
- the biological reactor has a ventilation system 41 at the bottom and an escape route of excess biological sludge 31, also at the bottom.
- a pulsation generator 121 is installed in the lower part of the membrane tank 111, near a communication channel 131 between the main space of the biological reactor 51 and the membrane tank. This access path 131 connects the lower part of the biological reactor 51 to the lower part of the membrane vessel 111.
- the pulsation generator is controlled by a controller 91.
- the liquid present in the membrane tank is placed in the presence of particles 71, in contact with the membranes 61.
- a gate 81 is installed on the recirculation zone 141 going from the upper part of the membrane 111 to the upper part of the biological reactor 51.
- the gate 81 serves as a separation system for particles and biological sludge, the particles being brought back by the gravity towards the membrane tank 111.
- the system operates using filtration elements in the form of hollow fibers.
- the pulsation generator 91 is here a pump, and that it may be a variant, in the different embodiments, of a Recirculated flow control device such as a damper, a variator or a bypass system.
- a hydrocyclone is used, the particles being recovered underflow and the sludge overflowing.
- a lamellar decanter is used at the top of the membrane vessel.
Landscapes
- Life Sciences & Earth Sciences (AREA)
- Biodiversity & Conservation Biology (AREA)
- Microbiology (AREA)
- Hydrology & Water Resources (AREA)
- Engineering & Computer Science (AREA)
- Environmental & Geological Engineering (AREA)
- Water Supply & Treatment (AREA)
- Chemical & Material Sciences (AREA)
- Organic Chemistry (AREA)
- Separation Using Semi-Permeable Membranes (AREA)
- Activated Sludge Processes (AREA)
Abstract
Description
Claims
Applications Claiming Priority (2)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR0857593A FR2938252B1 (fr) | 2008-11-07 | 2008-11-07 | Procede de traitement des eaux impliquant une filtration a travers au moins une membrane immergee |
PCT/FR2009/052143 WO2010052436A1 (fr) | 2008-11-07 | 2009-11-06 | Dispositif et procede de traitement des eaux impliquant une filtration a travers au moins une membrane immergee |
Publications (1)
Publication Number | Publication Date |
---|---|
EP2356080A1 true EP2356080A1 (fr) | 2011-08-17 |
Family
ID=40769576
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP09768155A Withdrawn EP2356080A1 (fr) | 2008-11-07 | 2009-11-06 | Dispositif et procede de traitement des eaux impliquant une filtration a travers au moins une membrane immergee |
Country Status (4)
Country | Link |
---|---|
US (1) | US20110210065A1 (fr) |
EP (1) | EP2356080A1 (fr) |
FR (1) | FR2938252B1 (fr) |
WO (1) | WO2010052436A1 (fr) |
Families Citing this family (2)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
FR3015463B1 (fr) | 2013-12-20 | 2016-01-29 | Veolia Water Solutions & Tech | Procede de traitement d'eau sur membranes integrant une adsorption sur materiau pulverulent adsorbant et des moyens permettant de limiter l'abrasion des membranes. |
CN105036296B (zh) * | 2015-05-04 | 2019-03-12 | 内蒙古工业大学 | 一种附加微通道湍流促进器的浸没式平板膜生物反应器 |
Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS63214177A (ja) * | 1987-03-02 | 1988-09-06 | Sanki Eng Co Ltd | メンブレンバイオリアクタ装置 |
Family Cites Families (8)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
DE2225973C2 (de) * | 1972-05-27 | 1974-07-04 | Merck Patent Gmbh, 6100 Darmstadt | Verfahren zum Beschichten von nicht porösem Material mit einer porösen Siliciumdioxidschicht |
US5932099A (en) * | 1995-07-25 | 1999-08-03 | Omnium De Traitements Et De Valorisation (Otv) | Installation for biological water treatment for the production of drinkable water |
US5879555A (en) * | 1997-02-21 | 1999-03-09 | Mockba Corporation | Electrochemical treatment of materials |
US20030132160A1 (en) * | 2002-01-11 | 2003-07-17 | Khudenko Boris M. | Membrane biotreatment |
US7118674B2 (en) * | 2004-10-14 | 2006-10-10 | Itt Manufacturing Enterprises, Inc. | Energy-efficient biological treatment with membrane filtration |
JP4835047B2 (ja) * | 2005-06-24 | 2011-12-14 | 富士ゼロックス株式会社 | 微粒子分散液の製造方法 |
FR2890389B1 (fr) * | 2005-09-08 | 2007-12-21 | Degremont Sa | Procede d'epuration biologique d'eaux usees avec ajout d'agent oxydant |
WO2009035700A2 (fr) * | 2007-09-12 | 2009-03-19 | Danisco Us Inc., Genencor Division | Filtration avec contrôle de l'encrassement interne |
-
2008
- 2008-11-07 FR FR0857593A patent/FR2938252B1/fr not_active Expired - Fee Related
-
2009
- 2009-11-06 WO PCT/FR2009/052143 patent/WO2010052436A1/fr active Application Filing
- 2009-11-06 EP EP09768155A patent/EP2356080A1/fr not_active Withdrawn
- 2009-11-06 US US13/128,313 patent/US20110210065A1/en not_active Abandoned
Patent Citations (1)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
JPS63214177A (ja) * | 1987-03-02 | 1988-09-06 | Sanki Eng Co Ltd | メンブレンバイオリアクタ装置 |
Also Published As
Publication number | Publication date |
---|---|
FR2938252B1 (fr) | 2014-08-22 |
WO2010052436A1 (fr) | 2010-05-14 |
US20110210065A1 (en) | 2011-09-01 |
FR2938252A1 (fr) | 2010-05-14 |
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