EP2046485A1

EP2046485A1 - Membrane reactor for the treatment of liquid effluents, comprising a membrane for diffusion of an oxidizing gas and a selective membrane, defining a reaction space between said membranes

Info

Publication number: EP2046485A1
Application number: EP07787909A
Authority: EP
Inventors: Samuel Heng; King Lun Yeung; Jean-Christophe Schrotter
Original assignee: OTV SA
Current assignee: Veolia Water Solutions and Technologies Support SAS
Priority date: 2006-08-01
Filing date: 2007-07-25
Publication date: 2009-04-15
Also published as: FR2904572B1; FR2904572A1; CN101516474A; WO2008015142A1; US20090321354A1

Abstract

The subject of the invention is a membrane reactor for the treatment of liquid effluents containing organic pollutants, of the type comprising at least one porous membrane (3) for the diffusion of an oxidizing gas, characterized in that it includes at least one selective membrane (2), (4) of said pollutants, which selective membrane defines, with said porous membrane for the diffusion of an oxidizing gas, a reaction space (31) into which said liquid effluents are injected, said reactor having means (34) for extracting retentates from said reaction space (31) and a space (32) for recovering the treated effluents, which space is separated from said reaction space (31) by said selective membrane or membranes (2), (4).

Description

Membrane reactor for the treatment of liquid effluents comprising a membrane for diffusing an oxidizing gas and a selective membrane defining between them a reaction space.

The field of the invention is that of the treatment of liquid effluents. More specifically, the invention relates to a membrane reactor used in particular, but not exclusively, for the treatment of liquid effluents containing organic pollutants that are difficult to biodegradable or non-biodegradable by an oxidation process alone (e.g., ozonation).

Currently, the treatment of liquid effluents containing organic compounds is mainly provided by biological channels.

These dies have the disadvantage of generating secondary waste in the form of sludge.

Despite this, biological treatment is often preferred over other processes because it is inexpensive. However, when toxic or non-biodegradable compounds are present in the effluent to be treated, the biological treatment becomes complex, if not impossible.

Depending on the concentration and the physicochemical properties of the organic pollutants in question, several alternative routes are possible, such as: - incineration; stripping; adsorption; filtration; chemical oxidation. Incineration is only possible in the particular case where the organic effluent is highly concentrated and has a sufficiently high heating value. However, incineration remains a particularly expensive process because it requires a furnace at high temperature (> 900 ⁰ C) coupled with a fume treatment process battery (VOC, N0χ, SOχ) which generate additional secondary waste. Stripping is possible only in the case where the organic pollutants are sufficiently concentrated and have a suitable Henry constant allowing them to be driven by a gas stream. In the end, a gas treatment step is therefore necessary, which tends to weigh down the corresponding processes and, consequently, the operating costs.

Adsorption is a simple solution to implement. However, this process has the disadvantage of generating a secondary solid waste which will then be incinerated and sent to a special industrial waste storage site. In the end, this solution is therefore expensive. Depending on the type of pollutants, membrane filtration processes such as micro filtration, ultrafiltration, nanofiltration or reverse osmosis are capable of separating solid and other soluble compounds from water with good efficiency. In addition to the fact that these processes remain relatively expensive, they have the disadvantage of concentrating and not destroying pollutants. Indeed, these are accumulated during filtration and must then undergo additional treatments.

Therefore, chemical oxidation processes are therefore the best existing solution for the destruction of non-biodegradable organic compounds. Of the chemical oxidation processes, the radical reactions initiated by the OH ° radicals such as: O ₃ , H ₂ O ₂ , O ₃ + UV, H ₂ O ₂ + O ₃ and TIO ₂ + UV are the most interesting.

Among the existing reagents, ozone stands out, proving less expensive and less restrictive than peroxide (H ₂ O ₂ ). Indeed, ozone can be produced on site as needed and requires no storage.

In addition, ozonation is already commonly used in the field of water treatment for the disinfection of drinking water. Its use in the treatment of industrial water is progressively spreading, in particular for the oxidation of non-biodegradable organic compounds. However, ozone is still relatively ineffective for the abatement and total mineralization of organic compounds.

In fact, because of the low solubility of ozone in the aqueous phases, the ozonation of the organic compounds does not always result in the total mineralization of the source pollutants. A number of intermediate by-products of degradation are thus formed during ozonation. These reaction by-products, the toxicity of which is not well known, must therefore be the subject of additional treatments as a precautionary principle.

Typically, adsorption, filtration and / or biological treatment steps can complete an ozonation process.

However, these complementary treatments increase the complexity of the processes and therefore at the same time their operating costs.

Also, to improve the reduction of non-biodegradable organic compounds by ozone, the use of heterogeneous catalysts and / or adsorbents in the form of grains or powders are often used.

However, the use of these heterogeneous compounds generates a subsequent filtration step or physicochemical separations to recover them.

Typically, the ozonation is carried out in a batch reactor or bubble column with porous diffusers or injector. Ozonation is used in pre or post treatment for the abatement of organic compounds or in order to increase their biodegradability.

Processes using ozone generally consist of several independent and distinct steps such as adsorption, filtration and / or biological treatment.

When the oxidizing gas is used in the presence of ozone-resistant filtration membranes, the introduction thereof is carried out upstream or possibly simultaneously. It should be noted that the ozone is then used as a cleaning agent, and its function is to limit the clogging of the membranes. Indeed, the bubbles and the hydrodynamics generated by them are favorable to detachment and degradation of the clogging layer.

It has also been proposed by the prior art to combine a filtration process with an oxidation reaction (catalytic or non-catalytic). This is described by patent documents FR-2 861 718 and WO-2005 047 191 which disclose a method and an installation using submerged membranes for the treatment of water. The continuous reactor contains catalysts and / or adsorbents in the form of a fluidized bed. Ozone is introduced into the reactor from below through the use of a porous diffuser. A separator membrane is used to retain catalytic or adsorbent materials in the reactor.

According to yet another technique described by the document TAKIZAWA "Membrane fouling by microfiltration with ozone scrubbing" (DESALINATION, ELSEVIER, AMSTERDAM, NL, vol.106, no.1, August 1996, pages 423-426), the decolouring power of ozone on filtration membranes used in a drinking water production process is studied. For this, a reactor incorporates in its lower part ozone diffusion means and in its upper part selective membranes.

In these two techniques, the reactor defines a single chamber integrating the oxidation treatment and filtration of the effluent. In other words, the oxidation and filtration steps take place within the same volume.

In practice, it is noted that the separating membrane does not allow selective concentration of the compounds and that the reactor does not generate synergy between oxidation and separation. In general, this technique does not improve the reduction of Total Organic Carbon (TOC).

Other effluent treatment techniques have been proposed by the prior art.

The patent document published under number US 5,580,452 describes a device for selectively transporting permeates from a fluid, integrating membrane modules. According to this technique, membrane elements each comprise two hollow tubular fibers. One of the two hollow fibers of each element is inserted into the other of the hollow fibers, an annular space extending between the two hollow fibers. A circulating liquid membrane system is formed by passing a liquid of selective permeability into the annular spaces.

The supply fluid flows through the central lumens. The purge fluid flows on the outer surface of the outer hollow fibers. When the feed fluid passes inside the inner tube, the permeate is separated from the feed fluid and transferred through the selective permeability liquid to the purge fluid. The passage of the permeate in the purge fluid is effected by the chemical potential differential through the selective permeability liquid. The hollow fibers placed at the interface between the feed fluid and the selective permeability fluid may consist of a polymeric material, metal or ceramic. The hollow fiber at the interface between the selective permeability liquid and the purge liquid may be hydrophobic or hydrophilic and may, for the purpose of selective gas separation, comprise a cobalt-based material for the purpose of separating oxygen from the air.

However, this technique does not provide for injecting (particularly in the central lumen) a strong oxidizer of such a nature as to oxidize pollutants. In addition, the porous fiber at the interface between the fluid to be treated and the selective permeability liquid does not constitute a selective membrane. Such a technique therefore does not allow:

selectively concentrating pollutant compounds;

to couple oxidation and separation steps. It has also been proposed by the prior art a technique, described by the document published under US-4,750,918, gas phase separation by selective permeability. The device implemented according to this technique comprises a transfer chamber inside which a liquid to be treated is introduced, hollow gas enrichment fibers and hollow gas abatement fibers extending across the transfer chamber. The flow of gas inside the fibers takes place in the opposite direction of the flow of gas inside the fibers. The countercurrent flow of gas in the fibers ensures a transfer of the gaseous phases between the liquid present in the transfer chamber and the hollow fibers. However, this technique is limited to exchanges between gaseous phases.

The invention particularly aims to overcome the disadvantages of the prior art.

More specifically, the invention aims to provide a membrane reactor that is more efficient than the reactors of the prior art. In this sense, the object of the invention is to provide such a reactor which makes it possible in particular to obtain a better reduction in COT.

The invention also aims to provide such a reactor that can reduce operating costs, particularly in terms of oxidizing gas consumption. The invention also aims to provide such a reactor that is simple in design, compact and inexpensive to achieve.

Another object of the invention is to provide such a reactor which is significantly less subject to clogging phenomena than known reactors.

These objectives, as well as others which will appear subsequently, are achieved thanks to the invention, which relates to a membrane reactor for the treatment of liquid effluents containing organic pollutants, of the type comprising at least one porous diffusion diffusion membrane. an oxidizing gas, characterized in that it comprises at least one membrane selective for said pollutants delimiting with said porous diffusion membrane of an oxidizing gas a reaction space in which said liquid effluents are injected, said reactor having means for extracting retentates from said reaction space and a treated effluent recovery space separated from said reaction space by said at least one selective membrane. Due to its particular configuration, the invention makes it possible to couple an oxidation reaction and a separation in the same confined module serving as a reactor. This concept of double membrane reactor allows simultaneously:

- the production of clean water; the production of a biodegradable treated effluent; an optimization of the ozone transfer rate of the gas phase in the liquid phase; an increase in the efficiency and kinetics of the oxidation reaction. Indeed, the coupling of the oxidation reaction and the membrane separation allows a significant improvement in the rate of reduction of organic compounds in solution compared to a conventional reactor.

Moreover, the use of ozone with an in situ membrane process also makes it possible to reduce the clogging of the membranes as already reported previously elsewhere.

It is noted that the invention makes it possible to optimize the oxidation reaction, in particular by virtue of: a transfer of the oxidizing gas increased by the large volume area ratio of the contactor constituted by the selective membrane; diffusion of the oxidizing gas directly into the reaction zone (less intermediate reaction); homogeneous mixing and diffusion;

- a control of the dose and the oxidation time. The invention also provides other advantages among which we can cite: the simplicity of the installation (a single module combining oxidation reaction and separation); the low cost of the installation; - the small size of the installation; a reduction in the reaction time and therefore the consumption of ozone;

- efficiency at an energy cost at least as good as conventional methods; - the production of filtered water containing no potentially toxic organic intermediates;

- production of treated water containing biodegradable organic compounds.

It is noted that, contrary to the techniques described by the documents FR-2 861 718 and "Membrane fouling degrowth by microfiltration with ozone scrubbing" cited above with reference to the prior art, the reactor according to the invention integrates compartmentalisation to optimize treatment and, in particular, the TOC reduction.

Indeed, the porous membrane and the selective membrane together define a closed space (with the exception of the effluent injection means and retentate extraction means generated by the selective membrane). In this space occurs the oxidation reaction, this confined in the vicinity of the selective membrane, which causes a synergy between separation and oxidation and a more effective reaction through the rapid evacuation of treated effluent (permeat). This synergy results in an acceleration of the reaction, followed by a rapid evacuation of the retentates.

In addition, another space, separated from the reaction space, is obtained by the compartmentalisation of the reactor: the recovery space treated effluents. For this, the selective membrane (s) constitute a partitioning between the reaction space and this recovery space.

In other words, a reactor according to the invention is defined as a membrane reactor for the treatment of liquid effluents containing organic pollutants, comprising at least one porous diffusion membrane of an oxidizing gas, comprising: a first compartment of which a first partition is constituted by said porous membrane and a second partition is constituted by at least one selective membrane through which said effluents are intended to circulate, means for injecting said effluents discharging into said first compartment and means for extracting retentates of pollutants, retained by said at least one selective membrane, extending from said first compartment, said first compartment forming a reaction space advantageously confined directly in the vicinity of said at least one selective membrane; a second compartment separated from said first compartment by said second partition, said second compartment forming a treated effluent recovery space.

According to a first embodiment, said porous membrane for diffusing an oxidizing gas defines a first closed perimeter, within which said selective membrane (s) extend (s) defining themselves a second closed perimeter. According to a second embodiment, said porous membrane for diffusing an oxidizing gas defines a first closed perimeter, outside of which said selective membrane or membranes extend defining a second closed perimeter.

According to a preferred solution, said porous membrane for diffusing an oxidizing gas and said selective membrane (s) are substantially cylindrical and concentric, and form three compartments constituting a basic module.

According to one conceivable variant, said porous diffusion membrane of an oxidizing gas and said selective membrane (s) are substantially plane, parallel and form three compartments constituting a basic module. The invention is not limited to such a configuration, the two membranes being, according to other embodiments conceivable to be perpendicular to each other, or consist of flat membranes, hollow fibers or cylindrical membranes, multichannels or spiral. According to a preferred embodiment, said porous membrane for diffusing an oxidizing gas and said selective membrane or membranes extend substantially vertically.

Thus, it ensures a good circulation and possible recycling of the oxidizing gas. The rise of the fine bubbles also ensures mixing, transfer and reaction of the oxidizing gas with the liquid phase.

Preferably, said porous membrane for diffusing an oxidizing gas is a porous ozone diffusion membrane.

It is noted that the oxidizing gas may, according to other embodiments conceivable, be:

- air, oxygen or a mixture; an injection of liquid product such as peroxide or sodium persulfate.

Advantageously, said selective membrane (s) belong to the following group: pervaporation membranes; ultrafiltration or microfiltration membranes; nanofiltration membranes; reverse osmosis membranes. According to a first embodiment, said selective membrane or membranes are inert, for example, based on metallic, ceramic or organic materials resistant to ozone.

According to a second embodiment, said selective membrane or membranes are active. In this way the reactor performance can be further improved.

In this case, according to a first variant, said at least one selective membrane and / or said at least one oxidizing gas diffusion membrane comprise at least one layer of an adsorbent material, advantageously belonging to the following group: activated carbon; any other inorganic or clay adsorbent material, preferably hydrotalcite or activated alumina. According to a second variant, said selective membrane or membranes comprise at least one layer of a catalyst, advantageously belonging to the following group:

- metals ;

- metal oxides. According to yet another conceivable variant, an adsorbent material and / or a catalyst are present in bed form in said reaction space.

According to another characteristic, the membrane reactor comprises means for recycling said oxidizing gas present in excess in said reaction space. According to a first configuration that can be envisaged, the reactor comprises several basic modules installed in series.

According to a second configuration that can be envisaged, the reactor comprises several basic modules installed in parallel.

Other characteristics and advantages of the invention will emerge more clearly on reading the following description of a preferred embodiment of the invention, given by way of illustrative and nonlimiting example, and the appended drawings among which: Figure 1 is a schematic longitudinal sectional view of a reactor according to the invention; Figure 2 is a schematic cross-sectional view of the membranes of a reactor according to the invention; Figure 3 is a graph showing the benefit of a reactor according to the invention compared to a simple ozonation. As described above, the principle of the invention lies in the fact of integrating, into a liquid effluent treatment reactor, two membranes, one for the diffusion of an oxidizing gas such as ozone, and the other for the separation of organic pollutants from effluents.

A preferred embodiment of the invention is illustrated in FIGS. 1 and 2.

As it appears, the reactor integrates two concentric porous membranes (or not); the first for the diffusion of ozone gas 3 in an aqueous medium and the second 2, 4 for the separation of water.

It is noted that the membranes together define three compartments (one for ozone, one for the water to be treated (and retentates), and the last for permeates), constituting a basic module.

The reactor can integrate several of these basic modules, arranged in series or in parallel.

The membranes 2, 4 and 3 delimit between them a reaction space 31 into which the effluents to be treated are injected by a feed A, the treated effluents D being recovered from a space 32 separated from the reaction space 31 by the membrane 2, 4.

In addition, a conduit 34 communicates with the space 31 to allow the extraction of retentates. It is therefore understood that the invention consists in designing a compartmentalized membrane reactor.

Indeed, the reaction space 31 constitutes a first compartment of which a partition is constituted by the ozone diffusion membrane 3 and another partition is constituted by the selective membrane 2, 4 (the ozone diffusion membrane and the selective membrane extending between wall portions of the reactor, in this case in the upper and lower parts of the reactor, these wall portions of the reactor therefore connecting the ozone diffusion membrane and the selective membrane to form a closed space).

In this first compartment open the injection means A effluents and retentates (consisting of the pollutants retained by the selective membrane) being extracted from this first compartment. Of course, the ozone diffusion membrane ensures the diffusion of ozone in this first compartment.

It should be noted that this compartment constitutes a confined reaction space, the ozone diffusion membrane being positioned relative to the selective membrane so that the oxidation reaction takes place completely or almost directly in the vicinity of the membrane. selective, in order to obtain the expected synergy between the oxidation and separation steps.

In addition, the reactor has a second compartment, separated from the first compartment by the partition formed by the selective membrane.

It is understood that the effluents flow from the first compartment to the second compartment by passing through the selective membrane, and the treated effluents are recovered from this second compartment.

This configuration as a whole makes it possible to improve and optimize the rate of transfer of ozone because of the much larger surface-to-volume ratio than in a conventional reactor.

As clearly shown in FIG. 2, the membrane 3 and the membrane 2, 4 are, according to the present embodiment, cylindrical and concentric, the membrane 3 defining a closed perimeter inside which the membrane 2 extends. , 4, itself defining a closed perimeter delimiting the space 32 of permeate recovery.

It should be noted that, according to another conceivable configuration, the membrane 3 defines a closed perimeter and the membrane 2, 4 extends outside the perimeter of the membrane 3 by defining itself a closed perimeter. Furthermore, the coupling of the action of the two membranes in the same module ie the diffusion of ozone gas coupled with a separation, is at the origin of a synergistic effect between the transfer and the consumption of ozone. Indeed, the concentration of organic compounds in the feed-side reaction space 31 in the confined space between the two membranes 3 and 2, 4 allows not only the increase of the ozone transfer factor but also an increased reaction kinetics compared to a conventional reactor without coupling.

The cylindrical reactor is positioned vertically. The membrane 2, 4 may be inert.

However, the performance of the membrane reactor can be improved by the addition of a layer 2 of materials, such as an adsorbent (activated carbon type, active alumina, hydrocalcites and other inorganic or clay materials) or catalysts (metal type or metal oxides) in the form of a bed in the reaction zone, and / or by grafting or coating these on a selective or non-selective membrane (thus on the membrane 3 and / or 2.4) serving as a contactor. This contactor may be of polymer ceramic or porous metal.

The selective membrane 2, 4 of pervaporation, ultrafiltration, microfiltration, nanofiltration or reverse osmosis is resistant to ozone. The presence of a selective membrane allows both a considerable improvement in the effectiveness of ozone for the removal of organic compounds in solution and also the production of clean water that does not contain organic compounds intermediate ozonation.

The diffusion of the ozone from the gas phase into the aqueous phase can be ensured by the use of a porous membrane diffuser made of porous polymer, steel or ceramic, an injector or a static contactor, in a bubble column or in a basin closed.

Different types of materials can serve as a diffuser for ozone.

For example, US Pat. No. 005645727 A discloses a process for producing ultra pure water with the use of a ceramic contactor. According to another technique described by Mitani. And Al (Mass transfer of ozone microporous diffusing reactor system, Ozone Sc Eng.27 (2005) 45-51), a cylindrical microporous steel membrane is placed in the center of a column. It has been shown that the rate of ozone transfer is significantly higher than conventional methods.

According to yet another technique described by R. H. S. Jansen, J. W. de

Rijj, A. Zwijnenburg, MHV Mulder, M. Wessling (Hollow Membrane Contactors - A means to study the reaction kinetics of humic substance ozonation, J. Memb., Sci., 257 (2005) 48-59), PVDF hollow fibers. are placed in a steel module that serve as contactor for ozone.

According to yet another technique described by Janknecht et al. (Ozonewater contacting by Ceramic Membranes, Separation and Purification Technology, 25 (2001) 341-346), have used ceramic membranes to distribute ozone in a tubular reactor, this effectively and for an energy consumption comparable to the others. methods of gas diffusion.

It is noted that, according to the embodiment illustrated in FIG. 1, the ozone is injected via a valve 6 coupled to a pressure gauge 7.

In addition, the reactor is equipped with means for detecting an excess of ozone in the reactor and means for recovering / recycling excess ozone.

In addition, the feed pipe is equipped with a measuring means

8 of a thermal torque which makes it possible to measure the temperature of the fluid to be treated.

The reactor illustrated in FIG. 1 and previously described has been implemented to show the advantages provided by the oxidation / separation coupling concept of the present invention.

For conducting the tests, a selective zeolite membrane on a ceramic support was used as a separator to concentrate the organic compounds and produce clean water. The separation method used was pervaporation (negative pressure).

The ozone used as oxidizing gas has been diffused through a porous steel membrane ensuring dissolution and mixing of the gas in the liquid.

Finally, phthalic acid (C ₆ H ₄ -COOH-COOK) (KHP) was used as a model pollutant for evaluation tests of the invention.

Indeed, the simple ozonation (without coupling with a separation) was compared to an ozonation coupled with a separation under the same experimental conditions:

[03] = 100 g / m3

Fo ₃ = 10-11 Ml / min

[KHP] = 0.53 g / L, equivalent to [COT] = 250 ppm carbon

T = 40 ⁰ C Figure 2 provides a comparison of the abatement performance of organic compounds (quantitatively measured by their TOC) with a reactor operating with coupling ozonation / separation and without coupling ozonation / separation.

For a residence time of the liquid of 3.3, 6.5 and 12.5 minutes, the percentage of reduction of the TOC with respect to the initial quantity were respectively 11, 25 and 66%; improvements of 34%, 52% and 120%, respectively, compared to the unlinked reactions under the same conditions.

In view of the results, it is clear that the coupling of the ozonation with the separation brings a not insignificant improvement. In addition, this improvement is all the more important as the residence time of the liquid in the reactor is long.

In fact, the production of water on the permeate side generates the concentration of organic compounds on the retentate side. This concentration results in an increase in the kinetics of degradation of the organic compounds dependent on it. This example shows that the invention makes it possible, in coupling oxidation and separation in a confined environment, to create a synergy between the two phenomena which results in a considerable improvement of the oxidation performance of the organic pollutants in solution.

Furthermore, it should be noted that the filtered water produced, on the permeate side, does not contain more than 2 ppm of carbon for a feed loaded up to 1000 ppm carbon.

These results are all the more remarkable that they were obtained with inert membranes. Much better performance is expected if the membrane is active, i.e. catalytic or adsorbent.

Claims

1. Membrane reactor for the treatment of liquid effluents containing organic pollutants, of the type comprising at least one porous membrane

(3) of diffusion of an oxidizing gas, characterized in that it comprises at least one selective membrane (2), (4) of said pollutants delimiting with said porous membrane (3) for diffusing an oxidizing gas a space of reaction (31) in which said liquid effluents are injected, said reactor having means for extracting (34) retentates from said reaction space (31) and a recovery space (32) of treated effluents separated from said reaction space (31) by said selective membrane (s) (2), (4).

Membrane reactor for the treatment of liquid effluents according to claim 1, characterized in that said porous membrane (3) for diffusing an oxidizing gas defines a first closed perimeter, within which said one or more selective membranes (2), (4) defining themselves a second closed perimeter.

Membrane reactor for the treatment of liquid effluents according to claim 1, characterized in that said porous membrane (3) for diffusing an oxidizing gas defines a first closed perimeter, outside which said one or more selective membranes (2), (4) defining themselves a second closed perimeter.

Membrane reactor for the treatment of liquid effluents according to one of claims 1 to 3, characterized in that said porous membrane (3) for diffusing an oxidizing gas and said selective membrane (s) (2), (4). ) are substantially cylindrical and concentric and form three compartments constituting a basic module.

Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 3, characterized in that said membrane porous (3) diffusion of an oxidizing gas and said selective membrane (s) (2), (4) are substantially flat, parallel and forming three compartments constituting a basic module.

6. Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 5, characterized in that said porous membrane (3) for diffusing an oxidizing gas is a porous ozone diffusion membrane.

7. Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 6, characterized in that said one or more selective membranes (2), (4) belong to the following group: pervaporation membranes; ultrafiltration or microfiltration membranes; nanofiltration membranes; reverse osmosis membranes.

8. Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 7, characterized in that said selective membrane (s) (2), (4) are inert.

9. Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 7, characterized in that said one or more selective membranes (2), (4) are active.

Membrane reactor for the treatment of liquid effluents according to claim 9, characterized in that said selective membrane (s) (2), (4) and / or said at least one porous oxidizing gas diffusion membrane (3) comprise at least one least one layer (2) of an adsorbent material.

Membrane reactor for the treatment of liquid effluents according to claim 10, characterized in that said adsorbent material belongs to the following group: activated carbon; or any other inorganic or clay material and preferably hydrotalcite or activated alumina.

Membrane reactor for the treatment of liquid effluents according to one of Claims 9 to 11, characterized in that the said selective membrane (s) (2), (4) comprise at least one layer of a catalyst.

13. Membrane reactor for the treatment of liquid effluents according to claim 12, characterized in that said catalyst belongs to the following group: metals; metal oxides.

14. Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 13, characterized in that an adsorbent material and / or a catalyst are present in bed form in said reaction space (31).

15. Membrane reactor for the treatment of liquid effluents according to any one of claims 1 to 14, characterized in that it comprises means for recycling said oxidizing gas present in excess in said reaction space.

16. Membrane reactor for the treatment of liquid effluents according to any one of claims 4 and 5, characterized in that it comprises a plurality of base modules installed in series.

17. Membrane reactor for the treatment of liquid effluents according to any one of claims 4 and 5, characterized in that it comprises a plurality of base modules installed in parallel.