EP4363104A1

EP4363104A1 - Method for the in situ regeneration of an adsorbent medium

Info

Publication number: EP4363104A1
Application number: EP22733688.0A
Authority: EP
Inventors: Olivier Danel; Isabelle Baudin; Laurent GUEY
Original assignee: Suez International SAS
Current assignee: Suez International SAS
Priority date: 2021-07-02
Filing date: 2022-07-01
Publication date: 2024-05-08
Also published as: AU2022301526A1; FR3124742A1; CN117940211A; WO2023275396A1

Abstract

The invention relates to a method for regenerating at least a portion of the adsorbent medium of at least one adsorption reactor implemented in a unit for treating a fluid, said regeneration method being carried out on the site of use of the adsorption reactor and comprising: - at least one step of removing at least a portion of the adsorbent medium from said at least one adsorption reactor, and - at least one chemical regeneration step comprising a step of bringing said portion of adsorbent medium into contact with a regeneration solution comprising water and sodium hydroxide. The invention also relates to a fluid-treatment method implementing the regeneration method, as well as to a fluid-treatment plant suitable for carrying out the fluid-treatment method according to the invention.

Description

DESCRIPTION

TITLE: ON-SITE ADSORBENT MEDIA REGENERATION PROCESS

TECHNICAL FIELD OF THE INVENTION

The invention relates to the field of fluid treatment systems, in particular water, implementing an adsorption step on an adsorbent medium. More particularly, the invention relates to a method for regenerating an adsorbent medium, on the site of use of the adsorbent medium, as well as a method for treating a fluid implementing said regeneration method. Finally, the invention also relates to an installation for implementing the regeneration process and an installation for implementing the process for treating a fluid.

STATE OF THE ART

For the treatment of fluid, and in particular for the production of drinking water or the treatment of effluents, it can be proposed to reduce the organic contaminants contained in raw water or effluent using a step of adsorption of this material on an adsorbent medium.

Indeed, the increasing load of organic contaminants (natural organic matter and micropollutants of anthropogenic or natural origin) observed in the resources leads drinking water producers and effluent treaters to rehabilitate their treatment channels, which have become unsuited to the objectives. quality. This increasing load of organic contaminants is also imposed on the producer of drinking water when designing a new treatment facility. Finally, effluent treaters, whether industrial or tertiary effluent before discharge into the natural environment or effluent to be made drinkable (wastewater) directly or indirectly (wastewater reuse), can also benefit from treatment taking into account a higher presence of organic contaminants. Taking into account this significant pollution by organic contaminants can in particular pass through the addition, from the design or during rehabilitation, of a refining process, in particular using activated carbon, such as in particular a filtration and/or adsorption by a bed of granular activated carbon (GAC).

In this field of water treatment, taking into account the emergence of organic micropollutants of synthetic origin still needs to be improved, especially when they are present in small quantities.

In particular, some of these emerging pollutants are poorly adsorbable, whether they are pollutants in the form of small molecules, polar molecules, or hydrophilic molecules. These include pesticide metabolites which can thus be found downstream of the adsorption step, such as an adsorption step with activated carbon in grains. The level of these emerging pollutants at the end of the treatment process can then exceed the regulatory thresholds if these pollutants are specifically regulated or in any event present a risk to be anticipated for emerging pollutants not yet regulated.

In fact, adsorbents, such as activated carbon, see their adsorption capacity decrease as they are used to adsorb pollutants.

Manufacturers implement operations to renew and/or regenerate the adsorbent media in order to increase the adsorption capacity of the adsorbent media.

Document WO2004/020349 discloses a process for regenerating adsorbent granular material by sampling and then chemical or thermal treatment of said material before reintroduction into the reactor.

State-of-the-art regeneration methods are generally implemented using complex and expensive techniques, requiring different solvents and/or a lot of energy, and transporting adsorbent media outside the treatment site of a fluid. .

There is therefore a need to propose a process for regenerating adsorbent media by a process that is simple to implement, with reduced energy requirements and not requiring the use of complex solvents.

SUMMARY OF THE INVENTION

The invention relates to a method for regenerating at least part of the adsorbent medium of at least one adsorption reactor implemented in a fluid treatment unit, said regeneration method being implemented on the site use of the adsorption reactor and comprising: at least one step of removing at least a portion of the adsorbent medium from said at least one adsorption reactor, and at least one step of chemical regeneration comprising a step of bringing into contact of said portion of adsorbent media with a regeneration solution comprising water and sodium hydroxide.

Preferably, said portion of adsorbent medium is taken from said at least one adsorption reactor and is introduced into a regeneration reactor before the regeneration step.

According to one embodiment of the invention, the regeneration solution is at a temperature less than or equal to 60° C., preferably ranging from 20 to 50° C., more preferably from 30 to 40° C. during the step of chemical regeneration. According to one embodiment of the invention, after contact with the regeneration solution, the adsorbent medium is rinsed using a rinsing solution, said rinsing solution preferably comprising water, even consisting of water.

Preferably, the chemical regeneration step further comprises a draining step at the end of the step of contact with the regeneration solution, said draining step being implemented before the rinsing step.

According to one embodiment of the invention, the regeneration method further comprises a step of electrochemical regeneration of the adsorbent medium carried out before or after or during the chemical regeneration step.

According to one embodiment of the invention, said portion of adsorbent media represents a quantity by volume less than or equal to 50% of the volume of absorbent medium, preferably a quantity by volume less than or equal to 30% of the volume of absorbent medium, preferably again a quantity by volume ranging from 1 to 10% of the volume of adsorbent medium.

According to one embodiment of the invention:

- the fluid to be treated is chosen from water, an urban effluent, an industrial effluent, preferably, the fluid to be treated is water, and/or

- the adsorbent medium is chosen from granular activated carbon, anion exchange resin, biomaterials, molecularly imprinted polymers and mineral materials, preferably the adsorbent medium is a granular activated carbon.

According to one embodiment of the invention, the regeneration process further comprises a step of introducing at least one portion of regenerated adsorbent medium into at least one adsorption reactor, identical to or different from the adsorption reactor containing the portion of adsorbent media that has been regenerated.

According to one embodiment of the invention, the regeneration method is implemented periodically, and comprises a step of determining the next regeneration step on the basis of the age of the adsorbent medium, characterized for example by the rate reduction in at least one target pollutant, and/or by the volume of bed treated and/or by the iodine index of the adsorbent medium.

According to one embodiment of the invention, the portion of adsorbent media sampled has an actual reduction rate of at least one target pollutant ranging from 40 to 80% and/or a bed volume treated by said adsorbent media ranges from 20 000 to 100,000 BVT (“bed volume treated” in English, more commonly referred to as “bed volume”, abbreviated respectively to BVT and BV)., preferably from 30,000 to 75,000 BVT, more preferably from 40,000 to 60 000 BVT and/or an iodine number ranging from 500 to 800 mg/g. The invention also relates to a method for treating a fluid in a treatment unit comprising at least one shutdown phase and at least one production phase, in which said at least one production phase comprises the passage of a fluid to be treated through a bed of adsorbent media within at least one adsorption reactor and in which said at least one shutdown phase comprises the implementation of a regeneration process according to the invention. For the duration of the remote regeneration (ie outside the adsorption reactor), the adsorption reactor can continue to produce; regeneration does not require stopping the treatment reactor.

According to one embodiment, part of the adsorbent medium, preferably granular activated carbon, is extracted from said processing unit during a production phase or when the unit is stopped, preferably during a production phase.

According to one embodiment of the invention, the process for treating a fluid further comprises a step for measuring the age of the adsorbent medium, preferably implemented by measuring the actual reduction rate in at least one target pollutant by the adsorbent medium, and/or by measurement of the bed volume treated by the adsorbent medium, and/or by measurement of the iodine number of the adsorbent medium.

The invention finally relates to a unit for processing a fluid for implementing the method according to the invention, said processing unit comprising:

- at least one reactor for adsorption of pollutants contained in the fluid to be treated, the reactor comprising within it an adsorbent medium,

- at least one means for taking adsorbent media from the adsorption reactor,

- at least one means of introducing adsorbent media into the adsorption reactor.

According to one embodiment of the invention, the processing unit according to the invention further comprises at least one regeneration reactor comprising an adsorbent media inlet pipe from said at least one adsorption reactor and a outlet making it possible to reintroduce the regenerated adsorbent medium into at least one adsorption reactor identical to or different from the adsorption reactor from which the absorbent medium to be regenerated originated.

The invention makes it possible to regenerate an adsorbent medium by a simpler process than those of the state of the art, which consumes less energy. In particular, the method of the invention makes it possible to regenerate the adsorbent media directly on the fluid treatment site, using less expensive reagents and a simplified installation since it makes it possible to dispense with heavy installations of storage of adsorbent media. Thus, in the context of the method of the invention, the adsorbent medium can be removed during a shutdown phase or a production phase of the treatment method and then directly reintroduced during this same shutdown phase or production phase, thus limiting the adsorbent media storage devices.

The regeneration process according to the invention can be implemented regularly, even on a poorly saturated adsorbent medium (relatively young age).

The regeneration method according to the invention makes it possible to improve the adsorption capacity of adsorbent media, thus allowing molecules that are difficult to adsorb to be adsorbed satisfactorily throughout the process for treating a fluid.

In particular, the regeneration process of the invention can be implemented easily and regularly in order to have a quality of adsorbent media, in terms of adsorption performance, which is almost constant, thanks to a regeneration implemented when the adsorbent media is far from being completely saturated (so-called young age adsorbent media).

BRIEF DESCRIPTION OF FIGURES

[Fig. 1] represents a diagram of a regeneration process according to the invention.

[Fig. 2] represents the efficiency coefficient of the regeneration process implemented with two different waters in the regeneration solution, evaluated for different pollutants.

[Fig. 3] represents the efficiency coefficient of the regeneration process implemented with two soda concentrations, evaluated for different pollutants.

[Fig. 4] represents the efficiency coefficient of the regeneration process implemented with three different quantities of regeneration solution, evaluated for different pollutants.

[Fig. 5] represents the efficiency coefficient of the regeneration process implemented with three GAC/soda contact times, evaluated for different pollutants.

[Fig. 6] represents the efficiency coefficient of the regeneration process after a rinsing step, evaluated for different pollutants.

[Fig. 7] represents the efficiency coefficient of the regeneration process after a static rinsing step implemented with two different rinsing waters, evaluated for different pollutants.

[Fig. 8] represents the efficiency coefficient of the regeneration process after a dynamic rinsing step implemented with two different rinsing waters, evaluated for organic matter.

[Fig. 9] represents the efficiency coefficient of the regeneration process, when the SAB test is implemented immediately or 24 hours after a regeneration step, evaluated for different pollutants.

[Fig. 10] represents the efficiency coefficient of the regeneration process, when the rinsing step is implemented immediately or 24 hours after a regeneration step, evaluated for different pollutants. DETAILED DESCRIPTION OF THE INVENTION

The invention relates to a method for regenerating an adsorbent medium used in the treatment of a fluid containing pollutants.

More specifically, the invention relates to a method for regenerating at least part of the adsorbent medium of at least one adsorption reactor implemented in a fluid treatment unit, said regeneration method being implemented on the site of use of the adsorption reactor and comprising:

- at least one step of sampling at least part of the adsorbent medium from said at least one adsorption reactor; and

- at least one chemical regeneration step comprising a step of bringing said portion of adsorbent media into contact with a regeneration solution comprising water and sodium hydroxide.

Adsorbent media

The invention can be implemented on different types of adsorbent media capable of eliminating different types of pollutants.

According to one embodiment of the invention, the adsorbent medium is chosen from granular activated carbon (GAC), anion exchange resin, biomaterials, molecularly imprinted polymers (MIP) and mineral materials.

Certain adsorbents such as modified clays and cyclodextrin polymers have also shown their effectiveness for certain specific micropollutants such as perfluorinated compounds (PFAs).

According to a particular embodiment, the adsorbent medium is activated carbon. Activated carbon is a material consisting essentially of carbonaceous matter with a porous structure. It can be produced in a known manner by pyrolysis of precursors of natural origin (wood, bark, coconut shells, coal, peat, cotton, organic matter of various origins, etc.) or of synthetic origin (polyacrylonitrile ( PAN), aramid fibres, etc.) already containing a significant proportion of carbon, this pyrolysis step being followed by a chemical or physical activation step.

Activated carbon is generally effective in removing long chain PFAS by hydrophobic interaction.

Biomaterials can also be implemented within the scope of the invention, including biochar. Biochar is a composition comprising pyrolyzed biomass biochar, biomass biochar produced by hydrothermal carbonization, or a combination thereof. The biomass can be chosen from waste from agricultural crops, forest waste, algae, animal or human waste, industrial waste, municipal waste, waste from anaerobic digesters, raw materials plants grown for biomass production, or a combination thereof. As an example, biochars made from hardwoods and pine trees can be considered. Biochar from rice husks can also be considered, in powder/granular form or in fiber form as in US2019270041 A1.

The biochar can be a powdered solid or granules. The biochar can also include a metal salt powder or granule. The metal salt can include iron, aluminum, calcium, magnesium, manganese, zinc, copper or a combination thereof, and in some examples the metal salt includes ferrous or ferric cations, ferrate anions, or a combination thereof. In particular embodiments, the metal salt includes ferric chloride.

According to a particularly preferred embodiment, the determination method of the invention is implemented to determine the remaining capacity of an adsorbent medium chosen from granular activated carbon (GAC), other aforementioned adsorbent media (clays, polymer, biochar... ). The method of the invention can be implemented with different types of CAG.

According to one embodiment, the adsorbent medium is chosen from granular activated carbon, anion exchange resin, biomaterials, molecularly imprinted polymers and mineral materials, preferably the adsorbent medium is a granular activated carbon.

For example, the granular activated carbon (GAC) that may come within the scope of the invention will typically have a particle size ranging from 300 to 2400 μm for at least 85 to 90% by weight of the grains. The dimensions given are those of the equivalent diameter of the grains for dry sieving or for wet sieving.

The adsorbent medium is implemented in at least one adsorption reactor. The fluid treatment unit within the scope of the invention may comprise one or more adsorption reactors, generally at least two adsorption reactors.

Fluid to be treated

The fluid to be treated within the framework of the invention can be water, in particular water to be made drinkable, but also an urban or industrial effluent (in particular leachates, which are liquid effluents from waste storage), before discharge in the natural environment or even effluents to be made drinkable (such as wastewater which is urban effluent) directly or indirectly (reuse of wastewater).

Preferably, the fluid to be treated is a liquid, such as water. According to a particularly preferred embodiment, the process of the invention is a drinking water treatment process. The water to be treated can be qualified as raw water, and can for example be taken from a watercourse, we will then speak of surface water, or be taken using a borehole, we will then speak of groundwater. The water to be treated can also be an effluent of urban origin (such as waste water otherwise called urban waste water) or industrial.

In the context of the present invention, the term “pollutant” denotes both organic matter and micropollutants. A micropollutant can be defined as an undesirable substance detectable in the environment at very low concentration (microgram per liter or even nanogram per litre). The presence of micropollutants in water is, at least in part, due to human activity (industrial processes, agricultural practices or drug and cosmetic residues). The micropollutant is characterized as being able, at these very low concentrations, to cause effects on living organisms due to its toxicity, its persistence and its bioaccumulation, or due to organoleptic nuisances (taste or smell, particularly relevant when is to treat water to be made drinkable). Micropollutants are very numerous (more than 110,000 molecules are listed by European regulations) and varied. The variety of pollutants makes it possible to classify them according to their origin, their nature, or even according to their very different chemical properties. Thus micropollutants can have a natural origin (such as compounds resulting from soil degradation, including geosmin or methylisoborneol or MIB, or bacterial residues), plant (such as algae metabolites including microcystins), animal, or human. Micropollutants can be classified according to their chemical nature, such as for example polar organic compounds, abbreviated as POC (from the English expression polar organic compounds) or organometallic compounds, abbreviated as MOC (from the English expression "metal organic compounds "). Micropollutants can have very different chemical properties, such as detergents, metals, hydrocarbons, pesticides, cosmetics or drugs. The proposed fluid treatment process therefore applies in particular to compounds of the pesticide type and to the associated metabolites. This process also applies particularly to solvents. This process is also particularly applicable to pharmaceutical residues or industrial activity residues. All of these categories of pollutants or micropollutants are thus specifically concerned by the present invention.

The treatment unit implemented in the context of the invention comprises at least one step for adsorption of pollutants contained in the fluid to be treated. This adsorption step is carried out using an adsorbent (or adsorbent medium).

Regeneration process The regeneration process according to the invention is implemented on the site of use of the adsorption reactor(s), within the fluid treatment unit. Thus, the invention makes it possible to limit or even eliminate steps for transporting adsorbent media to be regenerated or media that has already been regenerated.

The regeneration method comprises at least one step of removing at least part of the adsorbent medium from said at least one adsorption reactor.

Sampling can be carried out according to any method well known to those skilled in the art. Preferably, the removal of adsorbent media is carried out after washing the bed of adsorbent media.

Generally, the portion of adsorbent media removed is introduced into a regeneration reactor before the regeneration step. When there are several adsorption reactors, part of the adsorbent medium can be sampled from all or part of the reactors, preferably from part of the adsorption reactors.

In the case where the treatment unit comprises several adsorption reactors, a portion of adsorbent media can be taken from one or more of the adsorption reactors, then optionally mixed for the chemical regeneration step according to the invention.

Thus, the regeneration method according to the invention can be implemented in one or more regeneration reactors, preferably in a single regeneration reactor.

Preferably, for an adsorption reactor, the portion of adsorbent medium removed represents a quantity by volume less than or equal to 50% of the volume of absorbent medium, preferably quantity by volume less than or equal to 30% of the volume of absorbent medium, preferably again a quantity by volume ranging from 1 to 10% of the volume of adsorbent medium.

Water can be used to help the movement of the adsorbent media from the adsorption reactor to the regeneration reactor, this water can be called “motive water”. When the fluid to be treated is water, this motive water will preferably be taken from the fluid supply line upstream of the absorption reactor.

All or part of this motive water may possibly be evacuated before implementation of the regeneration stage. Indeed, the person skilled in the art will be able to adapt the quantity of water in the regeneration solution if all of the motive water is not evacuated before the regeneration step.

According to one embodiment, the sampling step is triggered periodically according to a regeneration frequency determined in advance.

According to one embodiment, the sampling step is triggered following a step for detecting a quality defect of the fluid to be treated downstream of the adsorption step, preferably the detection step comprises detection of a quality defect by comparison the level of pollutants or the number of pollutants between the upstream of the adsorption stage and the downstream of the adsorption stage.

The regeneration method according to the invention comprises at least one chemical regeneration step comprising a step of bringing said part of adsorbent medium into contact with a regeneration solution comprising water and sodium hydroxide.

Preferably, the regeneration solution consists of water and sodium hydroxide.

According to one embodiment, the mass concentration of sodium hydroxide in the regeneration solution is less than or equal to 20%, preferably less than or equal to 15%, more preferably ranges from 0.5% to 10%, or even 1.0 to 5% or 1.2 to 2.0%.

According to a preferred embodiment, the regeneration solution circulates through the adsorbent medium, preferably in a closed circuit.

Preferably, during the chemical regeneration step, the regeneration solution is at a temperature less than or equal to 60°C, preferably ranging from 20 to 50°C, more preferably from 30 to 40°C.

In the case where the fluid to be treated is water, the water of the regeneration solution can come from the fluid to be treated, thanks to a bypass upstream of the adsorption reactor on a supply line for the fluid to be treated .

At the end of the chemical regeneration, the regeneration solution can optionally be reused for one or more other regeneration steps. Indeed, the inventors have discovered that the regeneration step can be implemented using a regeneration solution that has already been used in a previous regeneration step. Thus, according to one embodiment, the regeneration solution implemented in the invention is chosen from a new regeneration solution (that is to say one that has not undergone regeneration) or a regeneration solution that has already been implemented in one or more chemical regeneration steps, for example in 1 to 4 regeneration steps. In the case where the process for treating a fluid aims to eliminate micropollutants, in particular micropollutants that are difficult to adsorb, the regeneration step can, according to a particular embodiment, be implemented using a regeneration solution having already been implemented in 1 to 4 regeneration steps.

According to one embodiment, the ratio between the mass in kg of adsorbent media to be regenerated and the volume in liters of regeneration solution used in total ranges from 1/20 to 20/1, preferably from 1/15 to 2/1 , or even from 1/10 to 1/1. According to one embodiment of the regeneration method according to the invention, after contact with the regeneration solution, the adsorbent medium is rinsed using a rinsing solution, which will typically circulate through the adsorbent medium , preferably in the same direction as the regeneration solution. Preferably, the rinse solution comprises water, preferably consists of water. When the fluid to be treated is water, this rinsing water will preferably be taken from the fluid supply line upstream of the absorption reactor.

According to one embodiment, the regeneration method further comprises a second rinsing step using a second rinsing solution (different from the first rinsing solution) comprising an acid solution. This acid rinsing step lowers the pH. When present, this acid rinsing step is followed by a water rinsing step to flush out the acid.

According to one embodiment, the rinsing step(s) is (are) implemented by circulating the rinsing solution through the bed of adsorbent media, preferably continuously. We will then speak of dynamic rinsing.

According to one embodiment of the regeneration process according to the invention, the chemical regeneration step further comprises a draining step at the end of the step of contact with the regeneration solution, said draining step being implemented before the rinsing step.

According to one embodiment, the draining step lasts from 1 hour to 72 hours, preferably from 5 hours to 48 hours, more preferably from 10 hours to 36 hours.

For this dewatering step, the regeneration solution can be removed from the regeneration reactor, for example by drainage, then the adsorbent media is maintained in the regeneration reactor. The inventors have indeed observed that this draining step makes it possible to further improve the regeneration process, in particular this step allows the regeneration solution still present within the adsorbent medium to continue to regenerate the adsorbent medium. During draining, if a small part of the regeneration solution is drained from the adsorbent media, this small part of the regeneration solution can be kept in the regeneration reactor.

According to one embodiment, the regeneration method according to the invention further comprises a step of electrochemical regeneration of the adsorbent medium carried out before or after or during the chemical regeneration step.

The regenerated adsorbent media is then typically reintroduced into at least one adsorption reactor. When the processing unit comprises several reactors adsorption, the regenerated adsorbent medium can be introduced into the same adsorption reactor or into a different absorption reactor from the adsorbent medium removed.

In the case where the treatment unit comprises several adsorption reactors, a portion of adsorbent media can be taken from several of the adsorption reactors, then mixed for the chemical regeneration step according to the invention. Thus, the regenerated adsorbent media will typically be reintroduced into one or more of the adsorption reactors from which the media to be regenerated was taken.

According to one embodiment, the portion of adsorbent medium sampled has a reduction rate in at least one target pollutant ranging from 40 to 80%. The target pollutant can be global organic matter or a specific micropollutant. Indeed, the regeneration method of the invention is particularly advantageous when it is implemented on a slightly used adsorbent medium.

Preferably, the regeneration method according to the invention is implemented periodically and comprises a step of controlling the frequency of regeneration as a function of the age of the adsorbent medium. The frequency between two regeneration cycles can be identical or different.

Preferably, the frequency of the implementation of the regeneration method according to the invention is adjusted according to the quality of the adsorbent medium, for example according to the age of the adsorbent medium.

The adsorbent medium typically exhibits a certain reduction in these adsorption capacities due to its use as an adsorbent of pollutants. This decrease in capacity is generally approached by the notion of productivity, itself assimilated to the age of the sample. The age of the sample, assimilated to its productivity, can thus be counted in bed volume treated (or “bed volume treated” in English, more commonly referred to as “bed volume”, abbreviated respectively as BVT and BV). The treated bed volume corresponds to the volume of fluid treated, more particularly water, by the adsorbent relative to the volume of the adsorbent. Thus, the higher the productivity of the adsorbent, the more the adsorbent has treated fluid, and the more it is worn, or older, and then we can assume that its adsorption capacities have decreased.

According to one embodiment of the invention, the quality of the adsorbent media is measured, typically monitored, in order to determine the age of the adsorbent media which can be defined by the actual rate of reduction in pollutant and/or by the volume of treated bed and/or by iodine number.

Thus, the regeneration process according to the invention makes it possible to rejuvenate the adsorbent media since, after introduction of a portion of regenerated media, the bed of adsorbent media of the adsorption reactor will have a younger age than the adsorbent media taken for the regeneration. The measurement of the actual reduction in a target pollutant of the adsorbent media can be followed in order to determine the age of the adsorbent media.

Preferably, the portion of adsorbent media sampled has a real reduction rate of at least one target pollutant ranging from 40 to 80%. According to one embodiment, the target pollutant is chosen from organic matter and micropollutants. Preferably, the target micropollutant is chosen from atrazine and atrazine derivatives (such as deisopropylatrazine, hydroxyatrazine, desethylatrazine), metolachlor, metolachlor OXA, metolachlor ESA, metazachlor OXA, chlortoluron, diuron , metaldehyde.

This measurement of pollutant reduction can in particular be carried out directly by comparing the concentrations of pollutants upstream and downstream of a treatment of a fluid using a sample of extracted adsorbent. The reduction in pollutants can also be measured indirectly, by measuring a level of pollutants using, for example, a method for measuring the iodine number or even by chromatography, mass spectrometry or spectroscopy. fluorescence (in particular by HPLC, HPLC-HR or HPLC-HR & MS). This level of pollutants thus determined can then be correlated with an actual concentration of pollutants, for example using predetermined charts in particular for each pollutant.

In the context of the present invention, a real reduction in at least one pollutant ranging from 40 to 80% means that at the time t considered, 40 to 80% in concentration of said pollutant is adsorbed by the adsorbent medium having the quality of the moment t.

The regeneration method according to the invention can thus comprise a step of measuring the (real) age of the adsorbent media and the duration before the next regeneration as well as the quantity of regenerated media reintroduced into an adsorption reactor can be determined by function of a target age to be reached for said adsorption reactor.

The regeneration method according to the invention can thus comprise the partial replacement of the adsorbent bed with adsorbent of young age (regenerated) until the target average age determined for the adsorbent bed is obtained. The amount of young adsorbent to be added is for example calculated using the arithmetic mean of the amount of spent adsorbent remaining in the bed and the amount of young adsorbent added to the bed.

According to one embodiment, to determine a target age at which to renew the carbon bed, the reduction in pollutants of the rejuvenated extracted adsorbent is qualified as “actual reduction in pollutants”. The abatement is qualified as real in that it is determined on the basis of a sample of the adsorbent actually used in the treatment process.

According to a particularly advantageous embodiment, the measurements of pollutant reductions of the adsorbent medium are implemented by adsorption tests in a short bed. Short bed adsorption corresponds to the English expression Short Bed Adsorber, abbreviated as SBA.

According to this embodiment, the frequency of the regeneration will then be set according to the reduction rate in at least one target pollutant. The removal of adsorbent media to be regenerated can then be triggered as soon as the reduction rate in at least one target pollutant is 40 to 80%, preferably 50 to 70%. According to one embodiment, the target pollutant is chosen from organic matter and micropollutants. Preferably, the target micropollutant is chosen from atrazine and atrazine derivatives (such as deisopropylatrazine, hydroxyatrazine, desethylatrazine), metolachlor, metolachlor OXA, metolachlor ESA, metazachlor OXA, chlortoluron, diuron , metaldehyde.

Other methods for measuring actual pollutant abatement can be used in the context of the present invention.

According to one embodiment, the actual abatement of at least one pollutant is determined by measurement and monitoring of at least one pollutant present in the fluid at the inlet of the adsorbent medium and measurement and monitoring of at least a pollutant present in the fluid at the outlet of the adsorbent medium.

Thus, it is possible, for example, to implement a continuous analyzer of the liquid or gas chromatography type, such as an online volatile organic compound (VOC) sensor, at the inlet and at the outlet of the reactor comprising the adsorbent medium. According to this embodiment, the pollutant(s) monitored can be chosen from pesticides, metabolites, solvents, industrial residues, and combinations thereof. The document US2019383779 describes a process for processing and monitoring pollutants online.

Regular analyses, for example by liquid or gas chromatography coupled with mass spectrometry, on the fluid at the inlet and on the fluid at the outlet can be implemented in order to compare the evolution of the content of at least one polluting.

Thus, the difference in concentration of at least one pollutant in the fluid at the inlet and in the fluid at the outlet thus makes it possible to quantify a real reduction in the pollutant(s) monitored.

Alternatively or in addition, the actual reduction in at least one pollutant can be quantified by monitoring a pilot unit (adsorption filtration column with the same adsorbent media as the industrial unit) supplied in parallel with the industrial unit, set up and dedicated specifically to monitoring the difference in fluid quality between the inlet and the outlet of this pilot bed and/or the quality of the media in this pilot bed. The age of the adsorbent media can be determined from the theoretical adsorption capacities for a treated bed volume.

According to one embodiment, the target age ranges from 20,000 to 100,000 BVT, preferably from 30,000 to 75,000 BVT, more preferably from 40,000 to 60,000 BVT. It will be necessary to reset the BVT at the end of each implementation of the regeneration method according to the invention.

According to this embodiment, the frequency of the regeneration will then be fixed according to the volume of bed treated. The withdrawal of adsorbent media to be regenerated can then be triggered as soon as the treated bed volume of the adsorbent media is from 20,000 to 100,000 BVT, preferably from 30,000 to 75,000 BVT, more preferably from 40,000 to 60,000 BVT.

The measurement of the treated bed volume can be coupled with the measurement of the actual reduction rate, and possibly with the quantity of fluid to be treated.

The iodine number can also be measured to determine the age of the adsorbent media. This iodine number is the quantity in milligrams of iodine adsorbed per gram of adsorbent and is used to quantify the adsorbent power of an adsorbent medium. For example for a new adsorbent, the iodine number can be higher than 950 or 1000 mg/g (as for the preferred activated carbon). Conversely, for a used adsorbent, the iodine number can be less than or equal to 500 mg/g. Regeneration of the adsorbent can then lead to recovery of an iodine number preferably greater than 600 mg/g or more preferably greater than 700 mg/g.

According to this embodiment, the frequency of regeneration will then be set according to the iodine number of the adsorbent medium. The removal of adsorbent media to be regenerated can then be triggered as soon as the iodine index is in the range of 500 to 800 mg/g.

In the context of the present invention, the iodine number can be determined according to the ASTM D4607 standard.

Other indices can be used to determine the age of the adsorbent media to be regenerated. Among these other indices, mention may be made, for example, of the methylene blue index, the phenol index, the molasses index, the tannic acid index, the monitoring of acetoxime dye. These other indices are determined by a measurement on a sample of adsorbent medium.

Thus, if the methylene blue index of the adsorbent medium is between 80 and 120 ml/g, then said adsorbent medium can be considered as an adsorbent medium of young age to be regenerated within the framework of the invention.

The methylene blue index of the adsorbent medium can be determined according to any method known to those skilled in the art. If the acetoxime index of the adsorbent medium is between 80 and 160, then said adsorbent medium can be considered as an adsorbent medium of young age to be regenerated within the scope of the invention.

The acetoxime index of the adsorbent medium can be determined using any method known to those skilled in the art.

If the molasses index of the adsorbent medium is between 50 and 150 mg/G, then said adsorbent medium can be considered as an adsorbent medium of young age to be regenerated within the framework of the invention.

The molasses index of the adsorbent medium can be determined using any method known to those skilled in the art.

Process for treating a fluid

The invention also relates to a process for treating a fluid in a treatment unit comprising at least one production phase, in which said at least one production phase comprises passing a fluid to be treated through a bed of media adsorbent within an adsorption reactor, said treatment method comprising at least one implementation of a regeneration method according to the invention.

Typically, the treatment process will also include at least one shutdown phase, said at least one shutdown phase preferably comprising a sequence for washing the media and possibly putting the unit out of production and implementing the process. regeneration according to the invention.

Said regeneration method according to the invention can be implemented during at least one production phase or a possible shutdown phase of the processing unit. Indeed, if the flow rate during the extraction of adsorbent media is not too high (for example thanks to a hydroejector), then it is possible to implement the regeneration process during a production phase.

The characteristics of the fluid, of the adsorbent medium and of the treatment unit defined in the context of the regeneration process are valid for the process for treating a fluid according to the invention. Thus, preferably, the adsorbent medium is chosen from granular activated carbon, anion exchange resin, biomaterials, molecularly imprinted polymers and mineral materials, preferably the adsorbent medium is granular activated carbon. Also, preferably, the fluid to be treated is water.

According to one embodiment, the treatment method according to the invention further comprises at least one stopping phase in which the bed of adsorbent media is washed using a washing solution. According to one embodiment, the process for treating a fluid comprises a step for controlling the quality of the adsorbent medium, for example by measuring the age of the adsorbent medium.

According to one embodiment, the treatment method according to the invention further comprises a step of measuring the age of the adsorbent medium, preferably implemented by measuring the actual reduction rate of at least one target pollutant by the adsorbent medium, and/or by measuring the bed volume treated by the adsorbent medium, and/or by measuring the iodine number of the adsorbent medium.

Preferably, the treatment method according to the invention comprises a measurement of the bed volume treated by the adsorbent medium which makes it possible to trigger the regeneration method.

According to this embodiment, the frequency of the regeneration will then be fixed according to the volume of bed treated. The withdrawal of adsorbent media to be regenerated can then be triggered as soon as the treated bed volume of the adsorbent media is from 20,000 to 10,0000 BVT, preferably from 30,000 to 75,000 BVT, more preferably from 40,000 to 60,000 BVT.

The measurement of the treated bed volume can possibly be coupled with the measurement of the actual reduction rate, and possibly with the quantity of the fluid to be treated.

According to one embodiment, the method for treating a fluid according to the invention is implemented within the framework of an activated carbon treatment method by ascending flow, as disclosed in document FR 3003477, cited above, and to which it is referred.

According to one embodiment, the process for treating a fluid according to the invention is implemented within the framework of a downflow activated carbon treatment process.

The present invention can also implement, in parallel with the processing unit, a pilot unit in which the same fluid to be treated circulates in a sample of the same adsorbent medium. Said pilot unit will thus typically comprise at least one means for measuring the age of the adsorbent media, said means for measuring the age can thus be implemented on the adsorbent media or on the treated fluid (at the outlet of the adsorbent media of the pilot unit). The pilot unit will thus be very representative of the "real" processing unit and will then make it possible to determine the age of the adsorbent medium and, depending on the age, to trigger a regeneration step as defined in the invention for the processing unit according to the invention.

Fluid treatment unit

The invention also relates to a fluid treatment unit for implementing the treatment method according to the invention, said treatment unit comprising: - at least one reactor for adsorption of pollutants contained in the fluid to be treated, the reactor comprising within it an adsorbent medium,

- at least one means for taking adsorbent media from the adsorption reactor,

Typically, the processing unit according to the invention further comprises at least one regeneration reactor comprising an inlet pipe for adsorbent media from said at least one adsorption reactor and an outlet pipe making it possible to reintroduce the regenerated adsorbent media in at least one adsorption reactor identical to or different from the adsorption reactor from which the absorbent medium to be regenerated originates.

The characteristics of the fluid, of the adsorbent medium and of the treatment unit defined within the framework of the regeneration process are valid for the treatment unit of a fluid according to the invention. Thus, preferably, the adsorbent medium is chosen from granular activated carbon, anion exchange resin, biomaterials, molecularly imprinted polymers and mineral materials, preferably the adsorbent medium is granular activated carbon.

According to one embodiment, the processing unit comprises at least two adsorption reactors, preferably at least three adsorption reactors. According to this embodiment with several adsorption reactors, the processing unit preferably comprises a single regeneration reactor.

According to one embodiment, the processing unit comprises a tank intended in particular for the preparation of the regeneration solution, said tank typically comprising heating means making it possible to heat the regeneration solution before contact with the adsorbent medium to be regenerated.

Preferably, the regeneration solution preparation tank feeds the regeneration reactor. The processing unit according to the invention may comprise a circulation loop between the tank for preparing the regeneration solution and the regeneration reactor.

When the regeneration is finished, the tank for preparing the regeneration solution can be emptied and replaced by the rinsing solution (implemented within the framework of the regeneration method according to the invention).

According to one embodiment, the processing unit comprises means for measuring the age of the adsorbent medium. Preferably, said means for measuring the age of the adsorbent media are chosen from among a UV spectroscope, a device for measuring dissolved organic carbon, a device for testing a short bed adsorber, and combinations thereof.

EXAMPLES Example 1: Treatment process according to the invention

A treatment method is for example implemented with the following characteristics: Adsorption reactor(s) o Total flow rate=1000-1200 m ³ /h and speed 10-15 m/h; o 4 granular activated carbon (GAC) reactors of 20 m ² each and 30 m ³ of GAC each; o Contact time of 6 to 9 minutes; o Maximum target VV = 50,000 VV (age of the media allowing the adsorption of targeted micropollutants and guaranteeing/controlling the quality of the water leaving the reactor); o GAC extraction of 4% vol every 8 days => 48,000 VV ± 1000 VV; Regeneration reactor(s):

1.2 m ³ of GAC - i.e. approximately 0.8 m ² (diameter 1 m) for 1.5 m in height,

Delay in the extractions between the reactors = approximately 2 days.

The [Fig. 1] is non-limiting and illustrates one embodiment of a treatment method according to the invention:

A. Operation in filtration:

The water at the inlet (EE) of the adsorbent medium (GAC for example) is introduced into at least one GAC reactor 1, 2, 3, 4, passes through at least one bed of activated carbon and exits through the ES line (outlet water).

B. Sampling of CAG (CAGp) from at least one of the CAG reactors 1, 2, 3, 4, typically after a washing step to extract media from the homogenized bed by washing/air stirring using the so-called motive water (EM). 100-150 g/l of GAC can be sampled.

C. Regeneration in regeneration reactor 5:

The media/regenerating solution contact time is 1 hour in a closed circuit, illustrated by circulation (Ce) and recirculation (Rc). The temperature of the regeneration solution is 40° C. (using a thermal resistor 10 for example) in a regeneration solution preparation device 6, and the regeneration solution consists of soda 8 at 1.7% (prepared for example with demined water 9).

At the end of the regeneration, the regenerating solution can be drained towards the rejection Rj (F), or directed towards a storage tank 7 for later reuse.

Typically, the adsorbent medium is then “drained” statically, preferably for 48 hours (time lag between 2 extractions).

D. Rinse (R):

The regenerated adsorbent media in the regeneration reactor can be rinsed, preferably with site water (EE, before GAC).

Rinsing can be carried out by dynamic contact (open circulation) by passing 2x 7 volumes of water per volume of GAC.

At the end of rinsing, the rinsing water can be evacuated towards the discharge Rj (F)

E. The media in "wet" mode after the rinsing step is then reinjected (CAGr) for example via hydro-injection with water from the site (EE before GAC) into at least one adsorbent reactor 1, 2, 3, 4, identical to or different from the adsorption reactor from which the medium is taken in step (B).

Example 2: Regeneration tests Protocol:

These tests were implemented with a CAG-type adsorbent media having an age of approximately 50,000 VV.

Regeneration solutions are obtained by diluting a 35% sodium hydroxide solution. 100 g of CAG to be regenerated are introduced with 800 mL of the solution prepared in a 1 L bottle (except for the example "effect of the mass ratio of CAG/volume of regeneration solution" where the quantity of solution is 200, 500 or 800mL). The bottles are placed in a rotating agitator where they are mixed at a speed of approximately 15 revolutions per minute.

For all tests, 100 g of GAC is weighed. 100 g of drained GAC corresponds to between 100 and 125 mL depending on the degree of humidity of the GAC.

After regeneration, it is possible to rinse the GAC to eliminate the soda that can still potentially act within the media, but above all to reduce the pH of the water leaving the filter or even to eliminate the desorbed dissolved compounds from the GAC pores.

Two ways of rinsing are studied in these tests: static rinsing and circulating rinsing. In both cases, the GAC is brought into contact with a certain volume of drilling water or demineralised water, once or several times.

• Static rinsing: the GAC is placed in a one liter bottle with water, without movement for several hours.

• Circulating rinse: the GAC is placed in a column with water. The water is pumped from the top of the column and then reinjected into the bottom of the column (or evacuated) via a peristaltic pump. The pump is configured to deliver a flow corresponding to a speed equivalent to that of the pilot (15 m/h).

The SBA, or Short Bed Adsorber Adsorber, is an adsorption test on unground GAC, in mini-columns, under implementation conditions close to those applied on a pilot scale. GAC, new, used or regenerated is placed in cartridges through which passes raw water spiked with micropollutants (feed matrix). The inlet water and the outlet water of each cartridge is analyzed to determine the reduction of micropollutants by the GAC, thus characterizing the adsorption capacities of the tested GAC. The peristaltic pump allows the passage of water at a fixed speed for a targeted contact time in the column, in ascending or descending flow.

For the conditions of the SBA test to be representative of those of the site, it is preferable to maintain an equivalent contact time, use the same input matrix and pass a minimum volume of 200 VV.

The raw water entering the SBA is spiked at 2.5 pg/L for micropollutants, such as pesticides or metabolites: Metolachlor OXA Metazachlor ESA, Alachlor OXA, Metolachlor ESA. The water is transferred to the GAC cartridges, and is analyzed as they enter and exit. For each sample, the concentration of micropollutants and organic matter (COD and UV absorbance) is measured.

The concentrations of water entering and leaving the control media (GAC before regeneration, partially saturated for the adsorption of certain micropollutants) and the reference media (new GAC) are also analyzed to determine the abatement rate, the coefficient of efficiency (RE) and maximum regeneration efficiency coefficient (RE max) for micropollutants and organic matter.

The 4 micropollutants mentioned were chosen because they are poorly adsorbable, i.e. they are associated with breakthroughs of GAC filters for productions or media age between 50,000 and 100,000 VV.

Organic matter (OM) is not harmful in itself but has many consequences on the treatment and appearance of water. It is, by reaction with oxidants (ozone, chlorine, etc.), the origin of disinfection by-products, it gives color to the water and is likely to saturate the filtering media.

In competition with micropollutants (concentration of micrograms per litre), MO (concentration of the order of milligrams per litre) is also adsorbed on GAC and can block access to certain pores.

It is therefore useful to reduce the organic matter to avoid saturating the GAC, the OM is monitored by UV spectroscopy analysis (at 254 nm) and measurement of DOC (Dissolved Organic Carbon). The higher the UV and COD values, the more MO is present.

The COD is measured after passing through a filter (TOC-meter).

Evaluation of performances The regeneration efficiency recovery coefficient (RE) was chosen to quantify the performance of the regeneration of GAC, vis-à-vis the adsorption of OM and micropollutants monitored in the project. It is calculated from the reduction of the compound monitored, on the regenerated CAG and on the control CAG. These quantities are therefore specific to each micropollutant (A).

The abatement of a compound: A = with Co the concentration of the compound at the inlet of the CAG filter and C the concentration of the compound at the outlet of the GAC filter.

The regeneration efficiency coefficient RE = ^{AQAG REGEWERE} with A the abatement of a

^A compound WITNESS CAG.

The maximum regeneration efficiency coefficient RE max = ^{Acag REGEWERE} ^A CAG NINE

To interpret the results, the RE of the regenerated GAC is compared to the RE limit = 100% and to the RE max for a given micropollutant according to the indications:

• If RE < 100%, the regenerated GAC has seen its adsorption capacity decrease.

• If RE = 100% the regeneration had no influence on the adsorption capacity.

• If RE > 100% the regenerated GAC has seen its adsorption capacity increase.

• If RE = RE max, the adsorption capacity found is equivalent to that of new GAC. This corresponds to the maximum possible value.

Effect of the nature of water

A regeneration step as described in this example was implemented for 7 hours, with a 1.7% concentrated sodium hydroxide solution using either demineralized water or borehole water (water from the site to be treated ). The efficiency coefficient RE has been determined for different pollutants and is shown in [Fig. 2]

The results show that the nature of the water has little influence on regeneration. Thus, preferably, the regeneration solution implemented in the invention comprises water from the treatment site, for example fluid to be treated in the case where the fluid to be treated is water, such as borehole water.

Effect of soda concentration

A regeneration step as described in this example was implemented for 7 hours, with a concentrated sodium hydroxide solution at 1.7% and 15.2%. The efficiency coefficient RE has been determined and is shown in [Fig. 3] The results of FIG. 3 show that there is a very small difference between a concentration of 1.7% and a concentration of 15.2%. Effect of the mass ratio of GAC/volume of regeneration solution

A regeneration step as described in this example was implemented with 100 g of CAG and different volumes of 1.7% regenerating solution: 200 ml_, 500 ml_ and 800 ml_. The efficiency coefficient RE was determined and is shown in [Fig. 4] The results of FIG. 4 show that the volume of regenerating solution has little influence on regeneration. Thus, the process has the advantage of being able to be implemented with a limited quantity of regeneration solution, thus reducing reagents and rejects.

Effect of contact time

A regeneration step as described in this example was implemented with different sodium hydroxide/GAC contact times under stirring), with a regenerating solution at

1.7%. The efficiency coefficient RE was determined and is shown in [Fig. 5] The results of FIG. 5 show that the regeneration duration has little influence on the regeneration efficiency.

Effect of rinsing

The effect of rinsing after the regeneration step was evaluated.

A static rinse was implemented for 7 hours (after a 7 hour regeneration with a 1.7% solution). The pH of the rinse solution (deionized water) decreases when the number of rinse VV increases. Thus, for 2VV the pH is 10.5, for 5VV the pH is 9.5 and for 10VV the pH is 9. The efficiency coefficient RE has been determined and is shown in [Fig. 6] The results of [Fig. 6] show that rinsing has little influence on regeneration efficiency.

Dynamic rinsing with closed circulation was implemented for 7h (after a 7h regeneration with a 1.7% solution). The pH of the rinse solution (site water) decreases as the number of rinse VV increases. Thus, for 2VV, the pH is

I I , for 5VV the pH is 9.5 and for 10VV the pH is 9.

Effect of rinse water

Static rinsing was implemented with demineralized water or 10VV site water for 7 hours (after regeneration for 7 hours with a 1.7% solution). The efficiency coefficient RE was determined and is shown in [Fig. 7]

Dynamic rinsing (closed circuit) was implemented with demineralized water or 10VV site water for 7 hours (after regeneration for 7 hours with a 1.7% solution). The efficiency coefficient RE has been determined and is shown in [Fig. 8] The results of Figs. 7 and Figs. 8 show that the nature of the rinsing water has little influence on the regeneration efficiency. Thus, according to a preferred embodiment of the invention, the rinsing water is site water (drilling water) originating from the fluid to be treated.

Effect of a draining step

The inventors discovered that a draining step (waiting time) before the rinsing step or the SBA test could be implemented in order to improve the efficiency of the regeneration.

An SBA test was implemented immediately after a 1 hour regeneration with a 1.7% regenerating solution and 24 hours after this regeneration in order to assess the effect of the draining step. The efficiency coefficient RE was determined and is shown in [Fig. 9] The results of FIG. 9 show that waiting 24 hours before carrying out an SBA test on the sample makes it possible to find a better adsorption capacity than when it is immediately tested in SBA. This result suggests that the soda within the "drained" media continues to act during this static phase after the initial phase of soda/media contact under agitation. The SBA test methodology applies a sample stabilization time of 200 VV which is similar to rinsing the media under test.

A rinsing step was implemented immediately after a 1 hour regeneration with a 1.7% regenerating solution or a rinsing step was implemented 24 hours after a 1 hour regeneration with a 1.7% regenerating solution. The efficiency coefficient RE was determined and is shown in [Fig. 10] where the result without rinsing with an immediate SBA is also indicated. The results of FIG. 10 show that a draining step before rinsing step makes the regeneration more efficient.

The invention thus proposes an effective regeneration process, implementing a reduced quantity of reagents and being able to use the water from the site as a rinsing solution and/or in the regeneration solution. In particular, the sodium hydroxide concentration may be less than 2% in the regeneration solution, in particular when the regeneration process includes a draining step (waiting) before rinsing.

Claims

1. Process for regenerating at least a portion of the adsorbent media of at least one adsorption reactor implemented in a fluid treatment unit, said regeneration process being implemented on the site of use of the adsorption reactor and comprising: at least one step of withdrawing at least part of the adsorbent medium from said at least one adsorption reactor, said part of adsorbent medium represents a quantity by volume less than or equal to 50% of the volume of absorbent media, and at least one chemical regeneration step comprising a step of bringing said portion of adsorbent media into contact with a regeneration solution comprising water and sodium hydroxide.

2. Regeneration process according to claim 1, in which said portion of adsorbent medium is taken from said at least one adsorption reactor and is introduced into a regeneration reactor before the regeneration step.

3. Regeneration process according to any one of claims 1 to 2, in which the regeneration solution is at a temperature less than or equal to 60° C., preferably ranging from 20 to 50° C., more preferably from 30 to 40°C during the chemical regeneration step.

4. Regeneration method according to any one of claims 1 to 3, wherein after contact with the regeneration solution, the adsorbent medium is rinsed using a rinsing solution, said rinsing solution preferably comprising water, or even consisting of water.

5. Regeneration process according to claim 4, in which the step of chemical regeneration further comprises a step of draining at the end of the step of contact with the regeneration solution, said step of draining being carried out work before the rinsing step.

6. Regeneration method according to any one of claims 1 to 5, further comprising a step of electrochemical regeneration of the adsorbent medium carried out before or after or during the chemical regeneration step.

7. Regeneration process according to any one of claims 1 to 6, in which the said portion of adsorbent media represents a quantity by volume less than or equal to 30% of the volume of absorbent medium, preferably a quantity by volume ranging from 1 to 10% the volume of adsorbent media.

8. Regeneration process according to any one of claims 1 to 7, in which:

9. Regeneration process according to any one of claims 1 to 8, further comprising a step of introducing at least a portion of regenerated adsorbent media into at least one adsorption reactor, identical or different from the reactor of adsorption containing the portion of adsorbent media that has been regenerated.

10. Regeneration method according to any one of claims 1 to 9, implemented periodically, comprising a step of determining the next regeneration step on the basis of the age of the adsorbent medium, characterized for example by the rate reduction in at least one target pollutant, and/or by the volume of bed treated and/or by the iodine index of the adsorbent medium.

11. Regeneration process according to any one of claims 1 to 10, in which the portion of adsorbent media sampled has an actual reduction rate of at least one target pollutant ranging from 40 to 80% and/or a bed volume treated with said adsorbent medium ranges from 20,000 to 100,000 BVT, preferably from 30,000 to 75,000 BVT, more preferably from 40,000 to 60,000 BVT and/or an iodine number ranging from 500 to 800 mg/g.

12. Process for treating a fluid in a treatment unit comprising at least one production phase, in which said at least one production phase comprises passing a fluid to be treated through a bed of adsorbent media within at least one adsorption reactor, said treatment method comprising at least one implementation of a regeneration method according to any one of claims 1 to 11.

13. Process for treating a fluid according to claim 12, further comprising a step of measuring the age of the adsorbent medium, preferably implemented by measuring the actual reduction rate of at least one target pollutant by the adsorbent medium, and/or by measuring the bed volume treated by the adsorbent medium, and/or by measuring the iodine number of the adsorbent medium.

14. Unit for processing a fluid for implementing the method according to claim 12 or 13, said processing unit comprising:

- at least one means for taking adsorbent media from the adsorption reactor,

15. Treatment unit according to claim 14, further comprising at least one regeneration reactor comprising an inlet pipe for adsorbent media from said at least one adsorption reactor and an outlet pipe making it possible to reintroduce the regenerated adsorbent media into at least one adsorption reactor identical to or different from the adsorption reactor from which the absorbent medium to be regenerated originates.