WO2006013235A1 - Method for depolluting organic micropollutant-containing fluid by activated carbon absorption in a processing reactor - Google Patents

Method for depolluting organic micropollutant-containing fluid by activated carbon absorption in a processing reactor Download PDF

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Publication number
WO2006013235A1
WO2006013235A1 PCT/FR2004/001735 FR2004001735W WO2006013235A1 WO 2006013235 A1 WO2006013235 A1 WO 2006013235A1 FR 2004001735 W FR2004001735 W FR 2004001735W WO 2006013235 A1 WO2006013235 A1 WO 2006013235A1
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WO
WIPO (PCT)
Prior art keywords
activated carbon
fluid
reactor
bed
water
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PCT/FR2004/001735
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French (fr)
Inventor
Jean Perot
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Societe D'amenagement Urbain Et Rural
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Publication date
Application filed by Societe D'amenagement Urbain Et Rural filed Critical Societe D'amenagement Urbain Et Rural
Priority to PCT/FR2004/001735 priority Critical patent/WO2006013235A1/en
Priority to FR0507163A priority patent/FR2874913B1/en
Publication of WO2006013235A1 publication Critical patent/WO2006013235A1/en

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    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F1/00—Treatment of water, waste water, or sewage
    • C02F1/28—Treatment of water, waste water, or sewage by sorption
    • C02F1/283—Treatment of water, waste water, or sewage by sorption using coal, charred products, or inorganic mixtures containing them
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2101/00—Nature of the contaminant
    • C02F2101/30—Organic compounds
    • C—CHEMISTRY; METALLURGY
    • C02—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F—TREATMENT OF WATER, WASTE WATER, SEWAGE, OR SLUDGE
    • C02F2103/00—Nature of the water, waste water, sewage or sludge to be treated
    • C02F2103/007—Contaminated open waterways, rivers, lakes or ponds

Definitions

  • the present invention relates to the general technical field of fluid treatment, such as water, containing organic micropollutants, especially water to drink or industrial water to recycle or reject in the environmental medium.
  • the present invention relates to a fluid depollution process containing organic micropollutants by adsorption on activated carbon in a treatment reactor.
  • the invention also relates to a fluid depollution installation containing organic micropollutants suitable for implementing said method.
  • Water such as water from surface water, must be treated and decontaminated to extract suspended solids, bacteria and residual organic and inorganic micropollutants before it can be used as drinking water. .
  • Industrial water must also be treated and decontaminated before it can be discharged into the environment.
  • Such processes generally require many reactors and structures to carry out the various processing steps, such as coagulation, flocculation, contact with the adsorbent powder or grain reagent, and decantation. These processes thus require heavy investments, both in GC and . equipment. Moreover, in such processes, the consumption of activated charcoal per cubic meter of treated water can reach several tens of milligrams per liter. The gradual saturation of activated carbon in grain organic compounds of natural origin or related to our human activities may represent a risk factor for premature leakage or release of undesirable micropollutants. In addition, activated carbon is an expensive material, which increases the price of. returns from the cubic meter of treated water.
  • the present invention fills this need.
  • the Applicant has thus discovered a novel process and an installation for efficiently treating and cleaning fluids containing organic micropollutants, such as surface water with a view to making them drinkable or industrial water, in an upflow treatment reactor. compact, very simple operation and implementation, and within which is effectively effected the separation of the fluids to be treated.
  • the method according to the present invention makes it possible in particular to carry out an efficient depollution of fluid, such as water, by adsorption on a moving bed of expanded activated carbon, as well as a gravitational separation of the treated fluid from the coal suspension within a single treatment structure, without significant loss of adsorbent, not requiring the addition of coagulation additives or flocculation, and without the obligation to equip the structure with a mechanical mixing device.
  • the process according to the present invention provides the possibility of continuously renewing the coal bed in the treatment reactor, by simply injecting new active carbon and extracting a corresponding amount of coal from the reactor, thus avoiding the saturation of the material, as may be the case with methods of the prior art grain activated carbon filtration.
  • Such a renewal of the coal bed according to the present invention is thus particularly advantageous since it constitutes in itself a mode of regeneration in situ of the coal bed.
  • the process provides for the possibility of partially recycling and regenerating the extracted used coal and reinjecting it into the reactor, and consequently reduces consumption. in new activated carbon.
  • the method according to the present invention thus makes it possible to treat surface waters to be watered, preferably previously clarified, or groundwater of low to medium turbidity, without specific pretreatments, and can then be followed directly by a filtration treatment, of the type filtration on granular media or membrane filtration type.
  • the process according to the present invention also makes it possible to treat various other types of water, such as water of industrial origin.
  • the present invention thus relates to a fluid depollution process containing organic micropollutants by adsorption on activated carbon in an upflow treatment reactor, comprising the injection of the fluid to be treated in the lower part of the reactor containing a bed of activated carbon. so as to create an expansion of said coal while simultaneously ensuring a gravitational separation between the activated carbon particles and the fluid, and the overflow recovery of the decanted and de-polluted fluid located in the upper part of the reactor overcoming the activated carbon bed.
  • the fluid to be treated is water, advantageously water to be watered, in particular groundwater or surface water, such as water of water. river, dam water, or alluvial water, or industrial water.
  • the method does not require the addition of any other coagulant and / or flocculant-type coagulant-type treatment additive.
  • the particle size of the active carbon and the upward velocity of the fluid are chosen so as to obtain an advantageously dense suspension of activated carbon expanded in the form of a moving bed, surmounted by a height of clear decanted fluid, the average concentration active carbon is advantageously between 100 and 300 g / 1 over the height of the expanded bed, and less than 2 mg / l in the upper part of the clear fluid zone surmounting the moving bed of activated carbon.
  • the moving bed of active activated carbon thus advantageously constitutes the reaction zone.
  • the particle size of the active carbon is between 100 and 800 ⁇ m, advantageously between 200 and 600 microns, even more advantageously between 200 and 400 microns, and the upward velocity of the fluid is between 2 and 20 m 3 / m 2 .h, advantageously between 8 and 15 m 3 / m 2 .h.
  • the contact time of the fluid with the activated carbon is defined as a function of the upward velocity of the fluid and the height of the expanded coal bed.
  • the contact time is between 5 and 60 min, advantageously between 5 and 30 min, more advantageously between 8 and 15 min.
  • the contact time may be greater than 60 min for certain types of fluids.
  • At least a portion of the active carbon is renewed periodically, by injecting new active carbon into the reactor, advantageously into the lower part of the coal bed, and by extracting a corresponding quantity of activated carbon. expanded.
  • at least a portion of the active activated carbon extracted from the reactor is conditioned in at least one storage tank, preferably for recycling purposes after partial regeneration and / or washing of the material.
  • the regeneration of the extracted activated carbon is advantageously based on the migration of micropollutants adsorbed on the surface of the coal grains towards the core of the grains, which takes place during the storage of the coal.
  • the washing of the extracted active carbon advantageously rests on the removal of the suspended matter of mineral or organic origin trapped by the activated carbon, by physical or hydraulic separation.
  • the purified coal can then be recycled to the reactor after passing through the storage tank. According to one variant, the purified coal is directly recycled to the reactor.
  • the washing of the active carbon is carried out within the treatment reactor itself, using a suitable washing system. Washing of the adsorbent material can then be achieved by introducing air and wash water to the reactor base.
  • the fact of washing or not the material and the washing method used is determined according to the nature of the fluid to be treated and the composition of the coal bed. For example, when treating clarified water from a treatment plant potabiliser, the coal bed can trap suspended solids, such as metal hydroxides, from the water to be cleaned.
  • the deconcentration of the activated carbon bed using large purge rates is a first solution to try to wash the activated carbon. However, such a solution often generates high consumption of activated carbon.
  • the introduction of a coal scrubbing system into or out of the process reactor is an advantageous means of reagent economy and process optimization in different applications.
  • the present invention also relates to a fluid depollution installation containing organic micropollutants comprising at least one treatment reactor (1) containing: fluid injection means (2) to be treated, located in a developed zone (3) in the lower part of the reactor and surmounted by a bed of activated carbon (4), - a recovery device (5) of the clear fluid decanted in the upper part of the reactor, injection means (6) of activated carbon new or regenerated and extraction means (7) of activated activated carbon, and optionally at least one storage tank for activated carbon.
  • This installation is suitable for implementing the method according to the present invention.
  • This installation also advantageously contains means for recirculating treated water inside the reactor, to prevent the reactor from being degraded during the production shutdown phases.
  • the fitted zone (3) contains a blocking bed, such as a bed of gravel surmounted by a bed of sand.
  • the treatment reactor (1) and the fluid injection means (2) are arranged in such a way as to obtain an upward fluid velocity of between 2 and 20 m 3 / m 2. h, advantageously between 8 and 15 m 3 / m 2 .h, when the particle size of the active carbon is between 100 and 800 microns, preferably between 200 and 600 microns.
  • the treatment reactor (1) is dimensioned in height and in section so as to obtain an expansion of the active carbon of between 20 and 300%, advantageously between 50 and 250%, when the speed ascensional fluid is between 2 and 20 m 3 / m 2 .h, preferably between 8 and 15 m 3 / m 2 .h.
  • the plant according to the present invention may contain a single treatment reactor or several associated processing reactors in parallel (flow sharing) or in series, especially in industrial applications. If the plant according to the present invention contains several treatment reactors, it is possible to selectively dimension each of the structures constituting the sector by selecting the composition of the coal bed (origin, grain size and quantity) and by adjusting the hydraulic operating parameters ( ascending speed and useful height of material in particular) and new adsorbent dosage.
  • the extracted used coal can be recycled with or without prior conditioning on the upstream reactors on the die, and reduce according to this working protocol the consumption of reagents.
  • the installation can comprise two treatment reactors within each of which are carried out a depollution of the fluid, as well as a separation between the activated carbon particles and the fluid.
  • the first treatment reactor can then be a roughing work where the majority of the organic pollution is clipped, and the second treatment reactor can be a refining work to remove the remaining pollutants.
  • FIG. 1 is a schematic sectional view of a fluid treatment reactor (1), stop, which comprises an injection ramp (2) of fluid to be treated, a developed zone (3) consisting of a bed of gravel and sand in the lower part of the reactor and surmounted by a bed of activated carbon (4) at rest, and a recovery device (5) of the clear fluid decanted in the upper part of the reactor.
  • stop which comprises an injection ramp (2) of fluid to be treated, a developed zone (3) consisting of a bed of gravel and sand in the lower part of the reactor and surmounted by a bed of activated carbon (4) at rest, and a recovery device (5) of the clear fluid decanted in the upper part of the reactor.
  • FIG. 2 is a schematic view of a reactor (1) for fluid treatment, in operation, which comprises a fluid injection manifold (2) to be treated, a developed zone (3) consisting of a bed of gravel and sand in the lower part of the reactor and surmounted by a bed of activated carbon (4) expanded, a recovery device (5) of the clear fluid decanted in the upper part of the reactor (1), and injection means ( 6) of new or regenerated activated carbon and extraction means (7) of activated activated carbon.
  • the process according to the present invention makes it possible to effectively treat various types of fluids, such as water, containing organic micropollutants, and especially natural and / or synthetic organic materials, as well as biodegradable compounds, in order to make these fluids drinkable.
  • the organic micropollutants of raw water can be of natural origin, which can come for example from algae, or can be linked to human agricultural or industrial activities. Such micropollutants can for example come from pesticides.
  • the treatment of fluids according to the present invention can be carried out continuously or discontinuously (batch type).
  • the batch treatment is advantageously used for water of industrial origin.
  • the treatment reactor (1) according to the present invention is advantageously a cylindrical reactor of vertical axis, a height generally between 2 and 5 meters, typically about 3 to 4 meters.
  • cylindrical is meant in the sense of the present invention a surface generated by a generator which moves parallel to a fixed direction by relying on a fixed plane profile perpendicular to the given direction.
  • the base of the treatment reactor (1) can be in various forms, such as the square or rectangular shape.
  • the fluid to be treated is introduced into the lower part of the reactor, preferably at the base of the reactor, in the developed zone (3).
  • the developed area (3) preferably contains a blocking bed, preferably consisting of a bed of gravel, surmounted by a bed of sand.
  • the blocking bed prevents the active carbon from entering the pipes used to inject the fluid to be treated.
  • the blocking bed also ensures the equidistribution of the fluid to be treated at any point on the surface of the bottom of the the work, and the suspension of the entire coal bed avoiding any dead fluid zone in the vicinity of the base of the coal bed.
  • the introduction of fluid is carried out by an injection ramp (2) equipped with orifices of adjusted diameter or with the aid of a strainer floor.
  • the introduction of fluid is carried out by distribution manifold and set of branches equipped with calibrated and staggered orifices embedded in the bed of gravel and directed towards the bottom.
  • the treatment reactor (1) according to the present invention contains a moving bed of activated carbon (4), preferably above the developed area (3).
  • the injection of activated carbon is carried out in the lower part of the reactor above the developed zone, preferably by a set of one to several injection canes.
  • the injection of fluid into the lower part of the reactor leads to an expansion of the adsorbent material by creating a mobile bed of expanded activated carbon, with the creation in parallel, and preferably simultaneously, of a water / coal bed interface.
  • a decreasing concentration gradient upwards can be created on the height of the moving bed, this concentration gradient varying according to the particle size distribution of the activated carbon used.
  • the particle size of the activated carbon and the upward velocity of the water are chosen so as to obtain a preferably dense suspension of activated carbon in the form of an expanded moving bed, surmounted by a height of clear decanted fluid.
  • fluid upward speed is meant in the sense of the present invention the ratio: hydraulic flow rate of the fluid on the ground surface of the treatment reactor.
  • the choice of a particular coal particle size associated with the choice of an upward velocity of the particular fluid allows a gravitational separation of the coal particles from the cleaned fluid with the obtaining of a clear fluid settled in the upper part. reactor, with very low residual active carbon content.
  • the particle size of the activated carbon is advantageously chosen so as to exert an effective adsorption of the micropollutants, while having an ability to expand, in order to create a mobile bed of coal by maintaining a dense suspension of activated carbon foam (Figure 2).
  • the activated carbon according to the present invention is typically of intermediate granulometry between that of activated carbon powder, which has a particle size in general of between a few microns and about 100 microns, and that of activated carbons grains, which have a particle size in general close mm.
  • the adsorbent content can reach several hundred grams per liter and effectively exert its depolluting action, without generating clogging or loss of load, as may be the case with the use of fixed bed systems.
  • no other processing additive than coal such as coagulants or flocculation agents for ballasting coal particles, needs to be added in the process according to the present invention.
  • coagulation or flocculation agents are added to treat certain types of fluids.
  • the treatment method according to the present invention can be carried out without a mixer, but it is also possible to provide an embodiment in which the treatment reactor contains a mechanical stirrer.
  • the clear decanted fluid is collected by overflow in the upper part of the reactor with the aid of a recovery device (5), such as a set of crenellated chutes.
  • At least a portion of the activated carbon is periodically renewed by injecting the new activated carbon into the reactor, and by extracting a corresponding amount of activated activated carbon.
  • the injection and extraction of activated carbon is typically done using metering pumps and ducts.
  • the renewal frequency varies according to the nature of the fluid to be treated, the selected coal and the level of pollution control sought.
  • Regenerated activated carbon may also be injected into the reactor, advantageously in addition to the new activated carbon.
  • the injection of new or regenerated activated carbon is advantageously carried out in the lower part of the activated carbon bed, where there is a high active carbon content, above the developed zone (3) advantageously containing a blocking bed.
  • the extraction of spent and used active carbon is carried out at a fixed or variable height, preferably at withdrawal levels placed above the top of the coal bed at the production stop (FIG. 1) and advantageously in a dense zone of coal.
  • the injection of new activated carbon with or without recycled coal into the reactor allows the continuous renewal of the coal suspension of the reactor.
  • the time allowed for this renewal can be likened to an age of suspension. It corresponds to the average residence time of the activated carbon particles inside the reaction zone constituted by the moving bed. It is adaptable to the nature of the fluid to be treated and the objectives of depollution sought. This renewal mode thus ensures consistent purification performance over time, avoiding the risk of premature leakage or release of undesirable micropollutants.
  • At least a portion of the active activated carbon extracted from the reactor can be packaged in at least one storage tank, advantageously for recycling purposes after partial regeneration and / or washing.
  • a fraction of the volume of the coal bed can thus be extracted periodically from the reactor to be stored under slow stirring in a storage tank, over a period of time adapted to the type of fluid to be treated.
  • Packaging then advantageously has the function of reducing the consumption of new coal, by allowing the recovery of a portion of the surface adsorption sites of the adsorbent material.
  • a few hours' storage of used and spent activated carbon allows the organic micropollutants adsorbed on the surface of the grains to migrate towards the heart of the grains.
  • washing of the adsorbent material is advantageously carried out in the context of the present invention, when the type of activated carbon used is capable of being charged with suspended matter of mineral or organic origin, before recycling the material into the reactor. treatment. Washing the extracted activated carbon is then preferably carried out by physical or hydraulic separation. Then, the purified coal, freed of a large fraction of impurities, is then recycled to the contact / separation structure, with or without passage into a storage tank. The recycling is preferably carried out in the treatment reactor by the circuit injection of activated carbon, with or without the addition of new or regenerated coal to compensate for losses.
  • the separation of the MES from the coal can be carried out according to another embodiment.
  • the washing of the activated carbon can thus be carried out inside the treatment structure, in particular by blowing air and washing water at the base of the reactor, after isolation of the structure, as is generally the case. practiced on grain activated carbon filters.
  • the water supply circuit to be treated is advantageously used for the introduction of washing water at the base of the reactor.
  • the washing air is injected with its own ramp and ramification device, or by the water supply circuit.
  • the sludge is evacuated in overflow of work and directed on the sludge die.
  • the treatment reactor (1) is dimensioned in height and in section so as to obtain an expansion of the active carbon of between 20 and 300%, advantageously between 50 and 250%, when the ascending velocity of the water is between 2 and 20 m 3 / m 2 .h, advantageously between 8 and 15 m 3 / m 2 .h.
  • An installation according to the present invention comprising a treatment reactor (1) containing at its lower end a developed zone (3) containing a bed of gravel surmounted by a bed of sand, whose packing height (gravel + sand) is 0.2 m. Above the developed area (3) is a bed of activated carbon (4) at a height of 0.7 m at rest ( Figure 1).
  • the active carbon introduced has a particle size of 0.4 to 0.8 mm.
  • the activated carbon concentration introduced is about 380 g / l when the reactor is stopped.
  • the treatment reactor (1) also contains injection means (2) for water to be treated in the developed area (3), injection means (6) and extraction (7) of the activated carbon, and a recovery device (5) of clear water decanted in the upper part of the reactor.
  • Such an installation is used to purify groundwater at a temperature of between 14 and 16 ° C.
  • the water is injected at the base of the treatment reactor (1) with a rate of rise of about 10 m 3 / m. 2 .h.
  • the resulting expansion rate is close to 70% ( Figure 2).
  • the decanted clear water located in the upper part of the reactor above the activated carbon bed (4), is recovered by overflow with a residual turbidity of less than 1 NFU and a MES content of less than or equal to 2 mg / l.
  • An installation according to the present invention comprising a treatment reactor (1) containing at its lower end a developed zone (3) containing a bed of gravel surmounted by a bed of sand, the packing height of which is 0.2 m .
  • the active carbon introduced has a particle size of 0.1 to 0.4 mm.
  • the activated carbon concentration introduced is about 380 g / l when the reactor is stopped. Such an installation is used to purify groundwater at a temperature between 14 and 16 ° C. Water is injected at the base of the reactor
  • the decanted clear water located in the upper part of the reactor above the activated carbon bed (4), is recovered by overflow with a residual turbidity of less than 1 NFU and a MES content of less than or equal to 2 mg / l.

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  • Life Sciences & Earth Sciences (AREA)
  • Hydrology & Water Resources (AREA)
  • Engineering & Computer Science (AREA)
  • Environmental & Geological Engineering (AREA)
  • Water Supply & Treatment (AREA)
  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Water Treatment By Sorption (AREA)

Abstract

The invention relates to a method for depolluting an organic micropollutant-containing fluid by activated carbon absorption in an upstream flow processing reactor consisting in injecting a processable fluid in to the lower part of the reactor comprising an activated carbon bed in such a way that the carbon expansion is produced, in simultaneously carrying out a gravity separation of the activated carbon particles and the fluid and in recovering a clarified and pollution-free fluid by overflowing in the top part of the reactor situated above the activated carbon bed. A device for depolluting an organic micropollutant-containing fluid for carrying out said method is also disclosed.

Description

Procédé de dépollution de fluide contenant des micropolluants organiques par adsorption sur charbon actif dans un réacteur de traitement Process for the depollution of fluid containing organic micropollutants by adsorption on activated carbon in a treatment reactor
La présente invention concerne le domaine technique général du traitement de fluide, tel que l'eau, contenant des micropolluants organiques, notamment de l'eau à potabiliser ou de l'eau d'origine industrielle à recycler ou rejeter dans le milieu environnemental.The present invention relates to the general technical field of fluid treatment, such as water, containing organic micropollutants, especially water to drink or industrial water to recycle or reject in the environmental medium.
En particulier, la présente invention concerne un procédé de dépollution de fluide contenant des micropolluants organiques par adsorption sur charbon actif dans un réacteur de traitement. L'invention a également pour objet une installation de dépollution de fluide contenant des micropolluants organiques convenant à la mise en œuvre dudit procédé.In particular, the present invention relates to a fluid depollution process containing organic micropollutants by adsorption on activated carbon in a treatment reactor. The invention also relates to a fluid depollution installation containing organic micropollutants suitable for implementing said method.
L'eau, telle que l'eau provenant des eaux de surface, doit être traitée et dépolluée, en vue d'en extraire les matières en suspension, les bactéries et les micropolluants résiduels organiques et minéraux, avant de pouvoir être utilisée comme eau potable. Les eaux industrielles doivent également être traitées et dépolluées, avant de pouvoir être rejetées dans le milieu environnemental.Water, such as water from surface water, must be treated and decontaminated to extract suspended solids, bacteria and residual organic and inorganic micropollutants before it can be used as drinking water. . Industrial water must also be treated and decontaminated before it can be discharged into the environment.
Divers procédés de traitement d'eau brute en vue de la rendre potable ont déjà été mis en œuvre. Sur les filières conventionnelles de traitement d'eau de surface, la clarification du liquide est souvent complétée par des traitements à l'aide de charbon actif sous forme de poudre. En outre, un traitement d'affinage à l'aide de charbon actif sous forme de grain est souvent réalisé en fîltration finale. De tels traitements d'élimination de micropolluants organiques par charbon actif induisent généralement des consommations importantes de réactifs, et une exploitation difficile en période de fortes variations de pollution organique sur le plan tant qualitatif que quantitatif.Various processes for treating raw water with a view to making it drinkable have already been implemented. On conventional surface water treatment systems, the clarification of the liquid is often completed by treatments using activated carbon in the form of powder. In addition, a refining treatment using activated carbon in the form of grain is often carried out in final filtration. Such treatments for the removal of organic micropollutants by activated charcoal generally induce large consumption of reagents, and difficult operation during periods of large variations in organic pollution both qualitatively and quantitatively.
De tels procédés nécessitent en général de nombreux réacteurs et ouvrages pour réaliser les diverses étapes du traitement, telles que la coagulation, la floculation, la mise en contact avec le réactif adsorbant en poudre ou en grain, et la décantation. Ces procédés nécessitent ainsi de lourds investissements, tant en GC qu'en. équipements. ' Par ailleurs, dans de tels procédés, les consommations en charbon actif ramenées au mètre cube d'eau traitée peuvent atteindre plusieurs dizaines de milligrammes par litre. La saturation progressive du charbon actif en grain en composés organiques d'origine naturelle ou liés à nos activités humaines peut représenter un facteur de risque de fuite prématurée ou de relargage de micropolluants indésirables. En outre, le charbon actif est un matériau cher, ce qui augmente le prix de . revient du mètre cube de l'eau traitée.Such processes generally require many reactors and structures to carry out the various processing steps, such as coagulation, flocculation, contact with the adsorbent powder or grain reagent, and decantation. These processes thus require heavy investments, both in GC and . equipment. Moreover, in such processes, the consumption of activated charcoal per cubic meter of treated water can reach several tens of milligrams per liter. The gradual saturation of activated carbon in grain organic compounds of natural origin or related to our human activities may represent a risk factor for premature leakage or release of undesirable micropollutants. In addition, activated carbon is an expensive material, which increases the price of. returns from the cubic meter of treated water.
Par conséquent, il existait ainsi un besoin de mettre au point un procédé et une installation pour le traitement de fluide, tel que l'eau, contenant des micropolluants organiques ne présentant pas les inconvénients des procédés et dispositifs de l'art antérieur, et permettant notamment de réaliser une dépollution et une séparation efficace du fluide au sein d'un seul ouvrage de traitement, en s 'affranchissant d'un ouvrage de décantation séparé.Therefore, there was thus a need to develop a method and a facility for the treatment of fluid, such as water, containing organic micropollutants not having the disadvantages of prior art methods and devices, and allowing in particular to perform a depollution and effective separation of the fluid within a single treatment structure, by avoiding a separate decantation work.
La présente invention vient combler ce besoin. Le Demandeur a ainsi découvert un nouveau procédé et une installation permettant de traiter et de dépolluer efficacement les fluides contenant des micropolluants organiques, telles que les eaux de surface en vue de les rendre potables ou les eaux industrielles, dans un réacteur de traitement à flux ascendant, compact, très simple d'exploitation et de mise en œuvre, et au sein duquel est réalisée de manière efficace la séparation des fluides à traiter.The present invention fills this need. The Applicant has thus discovered a novel process and an installation for efficiently treating and cleaning fluids containing organic micropollutants, such as surface water with a view to making them drinkable or industrial water, in an upflow treatment reactor. compact, very simple operation and implementation, and within which is effectively effected the separation of the fluids to be treated.
Le procédé selon la présente invention permet notamment de réaliser une dépollution efficace de fluide, tel que l'eau, par adsorption sur un lit mobile de charbon actif expansé, ainsi qu'une séparation gravitaire du fluide traité de la suspension de charbon au sein d'un seul ouvrage de traitement, sans perte sensible d'adsorbant, ne nécessitant pas l'ajout d'additifs de coagulation ou de floculation, et sans obligation d'équiper l'ouvrage d'un dispositif à mélange mécanique. Par ailleurs, le procédé selon la présente invention prévoit la possibilité de renouveler en continu le lit de charbon au sein du réacteur de traitement, par simple injection de charbon actif neuf et par extraction d'une quantité correspondante de charbon du réacteur, évitant ainsi la saturation du matériau, comme cela peut être le cas avec des procédés de l'art antérieur de filtration sur charbon actif en grain. Un tel renouvellement du lit de charbon selon la présente invention est ainsi particulièrement avantageux, puisqu'il constitue en soit un mode de régénération in situ du lit de charbon. De plus, le procédé prévoit la possibilité de recycler et de régénérer partiellement le charbon usagé extrait et de le réinjecter au sein du réacteur, et permet par conséquent de réduire les consommations en charbon actif neuf.The method according to the present invention makes it possible in particular to carry out an efficient depollution of fluid, such as water, by adsorption on a moving bed of expanded activated carbon, as well as a gravitational separation of the treated fluid from the coal suspension within a single treatment structure, without significant loss of adsorbent, not requiring the addition of coagulation additives or flocculation, and without the obligation to equip the structure with a mechanical mixing device. Furthermore, the process according to the present invention provides the possibility of continuously renewing the coal bed in the treatment reactor, by simply injecting new active carbon and extracting a corresponding amount of coal from the reactor, thus avoiding the saturation of the material, as may be the case with methods of the prior art grain activated carbon filtration. Such a renewal of the coal bed according to the present invention is thus particularly advantageous since it constitutes in itself a mode of regeneration in situ of the coal bed. In addition, the process provides for the possibility of partially recycling and regenerating the extracted used coal and reinjecting it into the reactor, and consequently reduces consumption. in new activated carbon.
Le procédé selon la présente invention permet ainsi de traiter des eaux de surface à potabiliser, de préférence préalablement clarifiées, ou des eaux souterraines peu à moyennement turbides, sans prétraitements spécifiques, et peut alors être suivi directement d'un traitement de filtration, du type filtration sur média granulaire ou de type filtration membranaire. Le procédé selon la présente invention permet également de traiter divers autres types d'eaux, telles que les eaux d'origine industrielle.The method according to the present invention thus makes it possible to treat surface waters to be watered, preferably previously clarified, or groundwater of low to medium turbidity, without specific pretreatments, and can then be followed directly by a filtration treatment, of the type filtration on granular media or membrane filtration type. The process according to the present invention also makes it possible to treat various other types of water, such as water of industrial origin.
La présente invention a ainsi pour objet un procédé de dépollution de fluide contenant des micropolluants organiques par adsorption sur charbon actif dans un réacteur de traitement à flux ascendant, comprenant l'injection du fluide à traiter en partie inférieure du réacteur contenant un lit de charbon actif de manière à créer une expansion dudit charbon en assurant parallèlement une séparation gravitaire entre les particules de charbon actif et le fluide, et la récupération par surverse du fluide décanté et dépollué situé en partie supérieure du réacteur surmontant le lit de charbon actif.The present invention thus relates to a fluid depollution process containing organic micropollutants by adsorption on activated carbon in an upflow treatment reactor, comprising the injection of the fluid to be treated in the lower part of the reactor containing a bed of activated carbon. so as to create an expansion of said coal while simultaneously ensuring a gravitational separation between the activated carbon particles and the fluid, and the overflow recovery of the decanted and de-polluted fluid located in the upper part of the reactor overcoming the activated carbon bed.
Dans un mode de réalisation particulier de la présente invention, le fluide à traiter est de l'eau, avantageusement de l'eau à potabiliser, en particulier de l'eau souterraine ou de l'eau de surface, telle que l'eau de rivière, l'eau de barrage, ou l'eau de nappe alluviale, ou de l'eau d'origine industrielle. Dans un mode de réalisation particulier de la présente invention, le procédé ne nécessite l'ajout d'aucun autre additif de traitement à effet lestant de type coagulant et/ou floculant.In a particular embodiment of the present invention, the fluid to be treated is water, advantageously water to be watered, in particular groundwater or surface water, such as water of water. river, dam water, or alluvial water, or industrial water. In a particular embodiment of the present invention, the method does not require the addition of any other coagulant and / or flocculant-type coagulant-type treatment additive.
Avantageusement selon la présente invention, la granulométrie du charbon actif et la vitesse ascensionnelle du fluide sont choisies de manière à obtenir une suspension avantageusement dense de charbon actif expansé sous forme de lit mobile, surmontée d'une hauteur de fluide clair décanté, la concentration moyenne en charbon actif étant avantageusement comprise entre 100 et 300 g/1 sur la hauteur du lit expansé, et inférieure à 2 m.g/1 en partie supérieure de la zone de fluide clair surmontant le lit mobile de charbon actif. Le lit mobile de charbon actif expansé constitue ainsi avantageusement la zone, réactionnelle.Advantageously according to the present invention, the particle size of the active carbon and the upward velocity of the fluid are chosen so as to obtain an advantageously dense suspension of activated carbon expanded in the form of a moving bed, surmounted by a height of clear decanted fluid, the average concentration active carbon is advantageously between 100 and 300 g / 1 over the height of the expanded bed, and less than 2 mg / l in the upper part of the clear fluid zone surmounting the moving bed of activated carbon. The moving bed of active activated carbon thus advantageously constitutes the reaction zone.
De manière encore plus avantageuse selon la présente invention, la granulométrie du charbon actif est comprise entre 100 et 800 μm, avantageusement entre 200 et 600 μm, encore plus avantageusement entre 200 et 400 μm, et la vitesse ascensionnelle du fluide est comprise entre 2 et 20 m3/m2.h, avantageusement entre 8 et 15 m3/m2.h.Even more advantageously according to the present invention, the particle size of the active carbon is between 100 and 800 μm, advantageously between 200 and 600 microns, even more advantageously between 200 and 400 microns, and the upward velocity of the fluid is between 2 and 20 m 3 / m 2 .h, advantageously between 8 and 15 m 3 / m 2 .h.
Avantageusement selon la présente invention, le temps de contact du fluide avec le charbon actif est défini en fonction de la vitesse ascensionnelle du fluide et de là hauteur du lit de charbon expansé.Advantageously according to the present invention, the contact time of the fluid with the activated carbon is defined as a function of the upward velocity of the fluid and the height of the expanded coal bed.
De manière encore plus avantageuse selon la présente invention, le temps de contact est compris entre 5 et 60 min, avantageusement entre 5 et 30 min, encore plus avantageusement entre 8 et 15 min. Le temps de contact peut être supérieur à 60 min pour certains types de fluides.Even more advantageously according to the present invention, the contact time is between 5 and 60 min, advantageously between 5 and 30 min, more advantageously between 8 and 15 min. The contact time may be greater than 60 min for certain types of fluids.
Selon une caractéristique particulière de la présente invention, au moins une partie du charbon actif est renouvelée périodiquement, par injection du charbon actif neuf dans le réacteur, avantageusement en partie inférieure du lit de charbon, et par extraction d'une quantité correspondante de charbon actif expansé. Dans un exemple de réalisation particulier de la présente invention, au moins une partie du charbon actif expansé extrait du réacteur est conditionnée dans au moins une cuve de stockage, avantageusement à des fins de recyclage après régénération partielle et/ou lavage du matériau. La régénération du charbon actif extrait est avantageusement basée sur la migration des micropolluants adsorbés en surface des grains de charbon vers le cœur des grains, qui s'effectue durant le stockage du charbon. Le lavage du charbon actif extrait repose avantageusement sur l'élimination des matières en suspension d'origine minérale ou organique piégés par le charbon actif, par séparation physique ou hydraulique. Le charbon épuré peut alors être recyclé dans le réacteur, après passage dans la cuve de stockage. Selon une variante, le charbon épuré est directement recyclé dans le réacteur.According to a particular characteristic of the present invention, at least a portion of the active carbon is renewed periodically, by injecting new active carbon into the reactor, advantageously into the lower part of the coal bed, and by extracting a corresponding quantity of activated carbon. expanded. In a particular embodiment of the present invention, at least a portion of the active activated carbon extracted from the reactor is conditioned in at least one storage tank, preferably for recycling purposes after partial regeneration and / or washing of the material. The regeneration of the extracted activated carbon is advantageously based on the migration of micropollutants adsorbed on the surface of the coal grains towards the core of the grains, which takes place during the storage of the coal. The washing of the extracted active carbon advantageously rests on the removal of the suspended matter of mineral or organic origin trapped by the activated carbon, by physical or hydraulic separation. The purified coal can then be recycled to the reactor after passing through the storage tank. According to one variant, the purified coal is directly recycled to the reactor.
Dans un autre mode de réalisation selon la présente invention, le lavage du charbon actif est réalisé au sein même du réacteur de traitement, à l'aide d'un système de lavage approprié. Le lavage du matériau adsorbant peut alors être réalisé par introduction d' air et d' eau de lavage à la base du réacteur. Le fait de laver ou non le matériau et le mode de lavage utilisé est déterminé en fonction de la nature du fluide à traiter et de la composition du lit de charbon. Par exemple, lors du traitement d'eau clarifiée d'une installation de traitement à potabiliser, le lit de charbon peut piéger les matières en suspension, du type hydroxydes métalliques, provenant de l'eau à dépolluer. La déconcentration du lit de charbon actif en utilisant des taux de purge importants est une première solution pour tenter de laver le charbon actif. Cependant, une telle solution génère souvent des consommations en charbon actif élevées. La mise en place d'un système de lavage du charbon au sein du réacteur de traitement ou à l'extérieur de celui-ci constitue un moyen avantageux d'économie de réactif et d'optimisation du procédé dans différentes applications.In another embodiment according to the present invention, the washing of the active carbon is carried out within the treatment reactor itself, using a suitable washing system. Washing of the adsorbent material can then be achieved by introducing air and wash water to the reactor base. The fact of washing or not the material and the washing method used is determined according to the nature of the fluid to be treated and the composition of the coal bed. For example, when treating clarified water from a treatment plant potabiliser, the coal bed can trap suspended solids, such as metal hydroxides, from the water to be cleaned. The deconcentration of the activated carbon bed using large purge rates is a first solution to try to wash the activated carbon. However, such a solution often generates high consumption of activated carbon. The introduction of a coal scrubbing system into or out of the process reactor is an advantageous means of reagent economy and process optimization in different applications.
La présente invention a également pour objet une installation de dépollution de fluide contenant des micropolluants organiques comprenant au moins un réacteur de traitement (1) contenant : des moyens d'injection (2) de fluide à traiter, situés dans une zone aménagée (3) en partie inférieure du réacteur et surmontée d'un lit de charbon actif (4), - un dispositif de récupération (5) du fluide clair décanté en partie supérieure du réacteur, des moyens d'injection (6) de charbon actif neuf ou régénéré, et des moyens d'extraction (7) de charbon actif expansé, et éventuellement au moins une cuve de stockage du charbon actif. Cette installation convient à la mise en œuvre du procédé selon la présente invention.The present invention also relates to a fluid depollution installation containing organic micropollutants comprising at least one treatment reactor (1) containing: fluid injection means (2) to be treated, located in a developed zone (3) in the lower part of the reactor and surmounted by a bed of activated carbon (4), - a recovery device (5) of the clear fluid decanted in the upper part of the reactor, injection means (6) of activated carbon new or regenerated and extraction means (7) of activated activated carbon, and optionally at least one storage tank for activated carbon. This installation is suitable for implementing the method according to the present invention.
Cette installation contient en outre avantageusement des moyens de recirculation d'eau traitée à l'intérieur du réacteur, pour éviter que le réacteur ne se dégrade pendant les phases d'arrêt de production. Dans un mode de réalisation particulier de la présente invention, la zone aménagée (3) contient un lit bloquant, tel qu'un lit de graviers surmonté d'un lit de sable.This installation also advantageously contains means for recirculating treated water inside the reactor, to prevent the reactor from being degraded during the production shutdown phases. In a particular embodiment of the present invention, the fitted zone (3) contains a blocking bed, such as a bed of gravel surmounted by a bed of sand.
Dans un mode de réalisation particulier de la présente invention, le réacteur de traitement (1) et les moyens d'injection (2) du fluide sont agencés de manière à obtenir une vitesse ascensionnelle du fluide comprise entre 2 et 20 m3/m2.h, avantageusement entre 8 et 15 m3/m2.h, lorsque la granulométrie du charbon actif est comprise entre 100 et 800 μm, avantageusement entre 200 et 600 μm. Selon une caractéristique particulière de la présente invention, le réacteur de traitement (1) est dimensionné en hauteur et en section de manière à obtenir une expansion du charbon actif comprise entre 20 et 300 %, avantageusement comprise entre 50 et 250 %, lorsque la vitesse ascensionnelle du fluide est comprise entre 2 et 20 m3/m2.h, avantageusement entre 8 et 15 m3/m2.h.In a particular embodiment of the present invention, the treatment reactor (1) and the fluid injection means (2) are arranged in such a way as to obtain an upward fluid velocity of between 2 and 20 m 3 / m 2. h, advantageously between 8 and 15 m 3 / m 2 .h, when the particle size of the active carbon is between 100 and 800 microns, preferably between 200 and 600 microns. According to one particular characteristic of the present invention, the treatment reactor (1) is dimensioned in height and in section so as to obtain an expansion of the active carbon of between 20 and 300%, advantageously between 50 and 250%, when the speed ascensional fluid is between 2 and 20 m 3 / m 2 .h, preferably between 8 and 15 m 3 / m 2 .h.
L'installation selon la présente invention peut contenir un seul réacteur de traitement ou plusieurs réacteurs de traitement associés en parallèle (partage du débit) ou en série, notamment dans des applications industrielles. Si l'installation selon la présente invention contient plusieurs réacteurs de traitement, il est possible de dimensionner sélectivement chacun des ouvrages constituant la filière en sélectionnant la composition du lit de charbon (origine, granulométrie et quantité) et en ajustant les paramètres de fonctionnement hydraulique (vitesse ascensionnelle et hauteur utile de matériau notamment) et de dosage en adsorbant neuf.The plant according to the present invention may contain a single treatment reactor or several associated processing reactors in parallel (flow sharing) or in series, especially in industrial applications. If the plant according to the present invention contains several treatment reactors, it is possible to selectively dimension each of the structures constituting the sector by selecting the composition of the coal bed (origin, grain size and quantity) and by adjusting the hydraulic operating parameters ( ascending speed and useful height of material in particular) and new adsorbent dosage.
En outre, lorsque plusieurs réacteurs sont disposés en série, le charbon usagé extrait peut être recyclé avec ou sans conditionnement préalable sur les réacteurs placés à l'amont sur la filière, et réduire suivant ce protocole de travail les consommations de réactifs.In addition, when several reactors are arranged in series, the extracted used coal can be recycled with or without prior conditioning on the upstream reactors on the die, and reduce according to this working protocol the consumption of reagents.
Typiquement, l'installation peut comprendre deux réacteurs de traitement au sein de chacun duquel sont réalisées une dépollution du fluide, ainsi qu'une séparation entre les particules de charbon actif et le fluide. Le premier réacteur de traitement peut alors constituer un ouvrage de dégrossissage où la majeure partie de la pollution organique est écrêtée, et le second réacteur de traitement peut constituer un ouvrage d'affinage afin d'éliminer les polluants restants.Typically, the installation can comprise two treatment reactors within each of which are carried out a depollution of the fluid, as well as a separation between the activated carbon particles and the fluid. The first treatment reactor can then be a roughing work where the majority of the organic pollution is clipped, and the second treatment reactor can be a refining work to remove the remaining pollutants.
Divers objets et avantages de la présente invention deviendront apparents pour l'homme dû métier par le biais de références aux dessins illustratifs suivants : la figure 1 est une vue schématique en coupe d'un réacteur (1) de traitement de fluide, à l'arrêt, qui comprend une rampe d'injection (2) de fluide à traiter, une zone aménagée (3) constituée d'un lit de graviers et de sable en partie inférieure du réacteur et surmontée d'un lit de charbon actif (4) au repos, et un dispositif de récupération (5) du fluide clair décanté en partie supérieure du réacteur. la figure 2 est une vue schématique d'un réacteur (1) de traitement de fluide, en fonctionnement, qui comprend une rampe d'injection (2) de fluide à traiter, une zone aménagée (3) constituée d'un lit de graviers et de sable en partie inférieure du réacteur et surmontée d'un lit de charbon actif (4) expansé, un dispositif de récupération (5) du fluide clair décanté en partie supérieure du réacteur (1), ainsi que des moyens d'injection (6) de charbon actif neuf ou régénéré et des moyens d'extraction (7) de charbon actif expansé.Various objects and advantages of the present invention will become apparent to those skilled in the art by reference to the following illustrative drawings: FIG. 1 is a schematic sectional view of a fluid treatment reactor (1), stop, which comprises an injection ramp (2) of fluid to be treated, a developed zone (3) consisting of a bed of gravel and sand in the lower part of the reactor and surmounted by a bed of activated carbon (4) at rest, and a recovery device (5) of the clear fluid decanted in the upper part of the reactor. FIG. 2 is a schematic view of a reactor (1) for fluid treatment, in operation, which comprises a fluid injection manifold (2) to be treated, a developed zone (3) consisting of a bed of gravel and sand in the lower part of the reactor and surmounted by a bed of activated carbon (4) expanded, a recovery device (5) of the clear fluid decanted in the upper part of the reactor (1), and injection means ( 6) of new or regenerated activated carbon and extraction means (7) of activated activated carbon.
Le procédé selon la présente invention permet de traiter efficacement divers types de fluides, tels que l'eau, contenant des micropolluants organiques, et notamment des matières organiques naturelles et/ou synthétiques, ainsi que des composés biodégradables, en vue de rendre ces fluides potables. Les micropolluants organiques des eaux brutes peuvent être d'origine naturelle, pouvant provenir par exemple d'algues, ou peuvent être liés aux activités humaines agricoles ou industrielles. De tels micropolluants peuvent ainsi par exemple provenir de pesticides.The process according to the present invention makes it possible to effectively treat various types of fluids, such as water, containing organic micropollutants, and especially natural and / or synthetic organic materials, as well as biodegradable compounds, in order to make these fluids drinkable. . The organic micropollutants of raw water can be of natural origin, which can come for example from algae, or can be linked to human agricultural or industrial activities. Such micropollutants can for example come from pesticides.
Le traitement des fluides selon la présente invention peut être réalisé en continu ou en discontinu (type batch). Le traitement en discontinu est avantageusement utilisé pour des eaux d'origine industrielle.The treatment of fluids according to the present invention can be carried out continuously or discontinuously (batch type). The batch treatment is advantageously used for water of industrial origin.
Le réacteur de traitement (1) selon la présente invention est avantageusement un réacteur cylindrique d'axe vertical, d'une hauteur en général comprise entre 2 et 5 mètres, typiquement d'environ 3 à 4 mètres. Par le terme de "cylindrique", on entend au sens de la présente invention une surface engendrée par une génératrice qui se déplace parallèlement à une direction fixe en s 'appuyant sur un profil plan fixe perpendiculaire à la direction donnée. Ainsi, la base du réacteur de traitement (1) peut se présenter sous différentes formes, telles que la forme carrée ou rectangulaire.The treatment reactor (1) according to the present invention is advantageously a cylindrical reactor of vertical axis, a height generally between 2 and 5 meters, typically about 3 to 4 meters. By the term "cylindrical" is meant in the sense of the present invention a surface generated by a generator which moves parallel to a fixed direction by relying on a fixed plane profile perpendicular to the given direction. Thus, the base of the treatment reactor (1) can be in various forms, such as the square or rectangular shape.
Le fluide à traiter est introduit en partie inférieure du réacteur, de préférence à la base du réacteur, dans la zone aménagée (3). La zone aménagée (3) contient de préférence un lit bloquant, avantageusement constitué d'un lit de graviers, surmonté d'un lit de sable. Le lit bloquant permet d'éviter que le charbon actif ne rentre dans les canalisations servant à injecter le fluide à traiter. Le lit bloquant permet d'assurer par ailleurs l'équirépartition du fluide à traiter en tout point de la surface du fond de l'ouvrage, et la mise en suspension de la totalité du lit de charbon en évitant toute zone de fluide morte au voisinage de la base du lit de charbon.The fluid to be treated is introduced into the lower part of the reactor, preferably at the base of the reactor, in the developed zone (3). The developed area (3) preferably contains a blocking bed, preferably consisting of a bed of gravel, surmounted by a bed of sand. The blocking bed prevents the active carbon from entering the pipes used to inject the fluid to be treated. The blocking bed also ensures the equidistribution of the fluid to be treated at any point on the surface of the bottom of the the work, and the suspension of the entire coal bed avoiding any dead fluid zone in the vicinity of the base of the coal bed.
Avantageusement selon l'invention, l'introduction de fluide, tel que l'eau, est réalisée par une rampe d'injection (2) équipée d'orifices de diamètre ajusté ou à l'aide - d'un plancher crépine. Encore plus avantageusement selon l'invention, l'introduction de fluide est réalisée par collecteur de répartition et jeu de ramifications équipées d'orifices calibrés et disposées en quinconce noyés au sein du lit de gravier et dirigés vers le fond.Advantageously according to the invention, the introduction of fluid, such as water, is carried out by an injection ramp (2) equipped with orifices of adjusted diameter or with the aid of a strainer floor. Even more advantageously according to the invention, the introduction of fluid is carried out by distribution manifold and set of branches equipped with calibrated and staggered orifices embedded in the bed of gravel and directed towards the bottom.
Le réacteur de traitement (1) selon la présente invention contient un lit mobile de charbon actif (4), avantageusement au-dessus de la zone aménagée (3).The treatment reactor (1) according to the present invention contains a moving bed of activated carbon (4), preferably above the developed area (3).
Avantageusement selon la présente invention, l'injection de charbon actif est réalisée en partie inférieure du réacteur au dessus de la zone aménagée, de préférence par jeu d'une à plusieurs canes d'injection.Advantageously according to the present invention, the injection of activated carbon is carried out in the lower part of the reactor above the developed zone, preferably by a set of one to several injection canes.
L'injection de fluide en partie inférieure du réacteur conduit à une expansion du matériau adsorbant en créant un lit mobile de charbon actif expansé, avec la création en parallèle, et de préférence simultanément, d'une interface eau/lit de charbon. Lors de l'expansion du charbon actif, un gradient de concentration décroissant vers le haut peut être créé sur la hauteur du lit mobile, ce gradient de concentration variant en fonction de la répartition granulométrique du charbon actif utilisée. Avantageusement selon la présente invention, la granulométrie du charbon actif et la vitesse ascensionnelle de l'eau sont choisies de manière à obtenir une suspension de préférence dense de charbon actif sous forme de lit mobile expansé, surmontée d'une hauteur de fluide clair décanté. Par le terme de "vitesse ascensionnelle du fluide", on entend au sens de la présente invention le rapport : débit hydraulique du fluide sur la surface au sol du réacteur de traitement.The injection of fluid into the lower part of the reactor leads to an expansion of the adsorbent material by creating a mobile bed of expanded activated carbon, with the creation in parallel, and preferably simultaneously, of a water / coal bed interface. During the expansion of the activated carbon, a decreasing concentration gradient upwards can be created on the height of the moving bed, this concentration gradient varying according to the particle size distribution of the activated carbon used. Advantageously according to the present invention, the particle size of the activated carbon and the upward velocity of the water are chosen so as to obtain a preferably dense suspension of activated carbon in the form of an expanded moving bed, surmounted by a height of clear decanted fluid. By the term "fluid upward speed" is meant in the sense of the present invention the ratio: hydraulic flow rate of the fluid on the ground surface of the treatment reactor.
Avantageusement selon la présente invention, le choix d'une granulométrie de charbon particulière associée au choix d'une vitesse ascensionnelle du fluide particulière permettent une séparation gravitaire des particules de charbon du fluide dépollué avec l'obtention d'un fluide clair décanté en partie supérieure du réacteur, à très faible teneur en charbon actif résiduel. La granulométrie du charbon actif est avantageusement choisie de manière à exercer une adsorption efficace des micropolluants, tout en ayant une aptitude à l'expansion, afin de créer un lit mobile de charbon en maintenant une suspension dense de charbon actif expansé (figure 2). Le charbon actif selon la présente invention est typiquement de granulométrie intermédiaire entre celle des charbons actifs en poudre, qui ont une granulométrie en général comprise entre quelques microns et 100 μm environ, et celle des charbons actifs en grains, qui ont une granulométrie en général proche du mm.Advantageously according to the present invention, the choice of a particular coal particle size associated with the choice of an upward velocity of the particular fluid allows a gravitational separation of the coal particles from the cleaned fluid with the obtaining of a clear fluid settled in the upper part. reactor, with very low residual active carbon content. The particle size of the activated carbon is advantageously chosen so as to exert an effective adsorption of the micropollutants, while having an ability to expand, in order to create a mobile bed of coal by maintaining a dense suspension of activated carbon foam (Figure 2). The activated carbon according to the present invention is typically of intermediate granulometry between that of activated carbon powder, which has a particle size in general of between a few microns and about 100 microns, and that of activated carbons grains, which have a particle size in general close mm.
Au sein du lit de charbon actif, en particulier dans sa partie inférieure, la teneur en adsorbant peut atteindre plusieurs centaines de grammes par litre et exercer efficacement son action dépolluante, sans engendrer de colmatage, ni de perte de charge, comme cela peut être le cas avec l'utilisation de systèmes à lit fixe. Par ailleurs, aucun autre additif de traitement que le charbon, tel que des agents de coagulation ou de floculation pour lester les particules de charbon, n'a besoin d'être ajouté dans le procédé selon la présente invention. On peut cependant avoir un mode de réalisation dans lequel des agents de coagulation ou de floculation sont ajoutés pour traiter certains types de fluides. Par ailleurs, le procédé de traitement selon la présente invention peut être réalisé sans mélangeur, mais on peut également prévoir un mode de réalisation dans lequel le réacteur de traitement contient un agitateur mécanique.In the bed of activated carbon, particularly in its lower part, the adsorbent content can reach several hundred grams per liter and effectively exert its depolluting action, without generating clogging or loss of load, as may be the case with the use of fixed bed systems. On the other hand, no other processing additive than coal, such as coagulants or flocculation agents for ballasting coal particles, needs to be added in the process according to the present invention. However, there may be an embodiment in which coagulation or flocculation agents are added to treat certain types of fluids. Moreover, the treatment method according to the present invention can be carried out without a mixer, but it is also possible to provide an embodiment in which the treatment reactor contains a mechanical stirrer.
Le fluide clair décanté est recueilli par surverse en partie supérieure du réacteur à l'aide d'un dispositif de récupération (5), tel qu'un jeu de goulottes crénelées.The clear decanted fluid is collected by overflow in the upper part of the reactor with the aid of a recovery device (5), such as a set of crenellated chutes.
Dans un mode de réalisation particulier de la présente invention, au moins une partie du charbon actif est renouvelée périodiquement par injection du charbon actif neuf dans le réacteur, et par extraction d'une quantité correspondante de charbon actif expansé. L'injection et l'extraction de charbon actif se font typiquement à l'aide de pompes doseuses et de conduits. La fréquence de renouvellement varie en fonction de la nature du fluide à traiter, du charbon sélectionné et du niveau de dépollution recherché. Du charbon actif régénéré peut également être injecté au sein du réacteur, avantageusement en complément du charbon actif neuf.In a particular embodiment of the present invention, at least a portion of the activated carbon is periodically renewed by injecting the new activated carbon into the reactor, and by extracting a corresponding amount of activated activated carbon. The injection and extraction of activated carbon is typically done using metering pumps and ducts. The renewal frequency varies according to the nature of the fluid to be treated, the selected coal and the level of pollution control sought. Regenerated activated carbon may also be injected into the reactor, advantageously in addition to the new activated carbon.
L'injection de charbon actif neuf ou régénéré est avantageusement effectuée en partie inférieure du lit de charbon actif, où se trouve une forte teneur en charbon actif, au-dessus de la zone aménagée (3) contenant avantageusement un lit bloquant.The injection of new or regenerated activated carbon is advantageously carried out in the lower part of the activated carbon bed, where there is a high active carbon content, above the developed zone (3) advantageously containing a blocking bed.
L'extraction de charbon actif expansé et usagé est réalisée à hauteur fixe ou variable, de préférence à des niveaux de soutirage placés au dessus du sommet du lit de charbon à l'arrêt de production (figure 1) et avantageusement en zone dense de charbon.The extraction of spent and used active carbon is carried out at a fixed or variable height, preferably at withdrawal levels placed above the top of the coal bed at the production stop (FIG. 1) and advantageously in a dense zone of coal.
L'injection de charbon actif neuf complémentée ou non de charbon recyclé dans le réacteur permet le renouvellement continu de la suspension de charbon du réacteur. Le temps imparti à ce renouvellement peut être assimilé à un âge de la suspension. Il correspond au temps de séjour moyen des particules de charbon actif à l'intérieur de la zone réactionnelle constituée par le lit mobile. Il est adaptable à la nature du fluide à traiter et des objectifs de dépollution recherchés. Ce mode de renouvellement permet ainsi d'assurer des performances épuratoires constantes dans le temps, en évitant les risques de fuites prématurées ou de relargage de micropolluants indésirables.The injection of new activated carbon with or without recycled coal into the reactor allows the continuous renewal of the coal suspension of the reactor. The time allowed for this renewal can be likened to an age of suspension. It corresponds to the average residence time of the activated carbon particles inside the reaction zone constituted by the moving bed. It is adaptable to the nature of the fluid to be treated and the objectives of depollution sought. This renewal mode thus ensures consistent purification performance over time, avoiding the risk of premature leakage or release of undesirable micropollutants.
Avantageusement selon la présente invention, au moins une partie du charbon actif expansé extrait du réacteur peut être conditionnée dans au moins une cuve de stockage, avantageusement à des fins de recyclage après régénération partielle et/ou lavage. Une fraction du volume du lit de charbon peut ainsi être extraite périodiquement du réacteur pour être stockée sous agitation lente dans une cuve de stockage, sur une durée adaptée au type de fluide à traiter. Le conditionnement a alors avantageusement pour fonction de réduire les consommations de charbon neuf, en permettant le recouvrement d'une partie des sites d'adsorption de surface du matériau adsorbant. Typiquement, un stockage de quelques heures du charbon actif expansé et usagé permet aux micropolluants organiques adsorbés à la surface des grains de migrer vers le cœur des grains. Il en résulte alors une régénération partielle du charbon actif par libération des sites d'adsorption de surface du charbon actif qui seront accessibles aux micropolluants à éliminer lorsque ce charbon sera recyclé dans le réacteur. Le lavage du matériau adsorbant est avantageusement mis en œuvre dans le cadre de la présente invention, lorsque le type de charbon actif utilisé est susceptible de se charger en matières en suspension d'origine minérale ou organique, avant de recycler le matériau dans le réacteur de traitement. Le lavage du charbon actif extrait est alors de préférence réalisé par séparation physique ou hydraulique. Ensuite, le charbon épuré, débarrassé d'une fraction importante d'impuretés, est alors recyclé sur l'ouvrage de contact/séparation, avec ou sans passage dans une cuve de stockage. Le recyclage est de préférence réalisé dans le réacteur de traitement par le circuit d'injection de charbon actif, avec ou sans apport de charbon neuf ou régénéré pour compenser les pertes.Advantageously according to the present invention, at least a portion of the active activated carbon extracted from the reactor can be packaged in at least one storage tank, advantageously for recycling purposes after partial regeneration and / or washing. A fraction of the volume of the coal bed can thus be extracted periodically from the reactor to be stored under slow stirring in a storage tank, over a period of time adapted to the type of fluid to be treated. Packaging then advantageously has the function of reducing the consumption of new coal, by allowing the recovery of a portion of the surface adsorption sites of the adsorbent material. Typically, a few hours' storage of used and spent activated carbon allows the organic micropollutants adsorbed on the surface of the grains to migrate towards the heart of the grains. This then results in a partial regeneration of the activated carbon by releasing active carbon surface adsorption sites which will be accessible to the micropollutants to be removed when this coal is recycled to the reactor. The washing of the adsorbent material is advantageously carried out in the context of the present invention, when the type of activated carbon used is capable of being charged with suspended matter of mineral or organic origin, before recycling the material into the reactor. treatment. Washing the extracted activated carbon is then preferably carried out by physical or hydraulic separation. Then, the purified coal, freed of a large fraction of impurities, is then recycled to the contact / separation structure, with or without passage into a storage tank. The recycling is preferably carried out in the treatment reactor by the circuit injection of activated carbon, with or without the addition of new or regenerated coal to compensate for losses.
Avantageusement selon la présente invention, la séparation des MES du charbon peut être réalisée suivant un autre mode de réalisation. Le lavage du charbon actif peut ainsi être effectué à l'intérieur de l'ouvrage de traitement, notamment par insufflation d'air et d'eau de lavage à la base du réacteur, après isolement de l'ouvrage, comme cela est en général pratiqué sur les filtres à charbon actif en grain. On utilise avantageusement le circuit d'alimentation d'eau à traiter pour l'introduction d'eau de lavage à la base du réacteur. L'air de lavage est injecté avec son propre dispositif de rampe et de ramifications, ou par le circuit d'alimentation d'eau. Les boues sont quant à elles évacuées en surverse d'ouvrage et dirigées sur la filière boues.Advantageously according to the present invention, the separation of the MES from the coal can be carried out according to another embodiment. The washing of the activated carbon can thus be carried out inside the treatment structure, in particular by blowing air and washing water at the base of the reactor, after isolation of the structure, as is generally the case. practiced on grain activated carbon filters. The water supply circuit to be treated is advantageously used for the introduction of washing water at the base of the reactor. The washing air is injected with its own ramp and ramification device, or by the water supply circuit. The sludge is evacuated in overflow of work and directed on the sludge die.
Avantageusement selon la présente invention, le réacteur de traitement (1) est dimensionné en hauteur et en section de manière à obtenir une expansion du charbon actif comprise entre 20 et 300 %, avantageusement comprise entre 50 et 250 %, lorsque la vitesse ascensionnelle de l'eau est comprise entre 2 et 20 m3/m2.h, avantageusement entre 8 et 15 m3/m2.h.Advantageously according to the present invention, the treatment reactor (1) is dimensioned in height and in section so as to obtain an expansion of the active carbon of between 20 and 300%, advantageously between 50 and 250%, when the ascending velocity of the water is between 2 and 20 m 3 / m 2 .h, advantageously between 8 and 15 m 3 / m 2 .h.
Les exemples suivants sont donnés à titre non limitatif et illustrent la présente invention.The following examples are given without limitation and illustrate the present invention.
Exemples de réalisation de l'invention :Examples of embodiment of the invention:
Exemple 1 :Example 1
Une installation selon la présente invention, comprenant un réacteur de traitement (1) contenant à son extrémité inférieure une zone aménagée (3) contenant un lit de graviers surmonté d'un lit de sable, dont la hauteur de garnissage (gravier + sable) est de 0,2 m. Au dessus de la zone aménagée (3), se trouve un lit de charbon actif (4) d'une hauteur de 0,7 m au repos (Figure 1). Le charbon actif introduit a une granulométrie de 0,4 à 0,8 mm. La concentration en charbon actif introduite est d'environ 380 g/1, lorsque le réacteur est à l'arrêt. Le réacteur de traitement (1) contient également des moyens d'injection (2) d'eau à traiter dans la zone aménagée (3), des moyens d'injection (6) et d'extraction (7) du charbon actif, ainsi qu'un dispositif de récupération (5) de l'eau claire décantée en partie supérieure du réacteur.An installation according to the present invention, comprising a treatment reactor (1) containing at its lower end a developed zone (3) containing a bed of gravel surmounted by a bed of sand, whose packing height (gravel + sand) is 0.2 m. Above the developed area (3) is a bed of activated carbon (4) at a height of 0.7 m at rest (Figure 1). The active carbon introduced has a particle size of 0.4 to 0.8 mm. The activated carbon concentration introduced is about 380 g / l when the reactor is stopped. The treatment reactor (1) also contains injection means (2) for water to be treated in the developed area (3), injection means (6) and extraction (7) of the activated carbon, and a recovery device (5) of clear water decanted in the upper part of the reactor.
Une telle installation est utilisée pour épurer de l'eau souterraine à une température comprise entre 14 et 16 0C. L'eau est injectée à la base du réacteur de traitement (1) avec une vitesse ascensionnelle d'environ 10 m3/m2.h. Le taux d'expansion résultant est voisin de 70% (Figure 2).Such an installation is used to purify groundwater at a temperature of between 14 and 16 ° C. The water is injected at the base of the treatment reactor (1) with a rate of rise of about 10 m 3 / m. 2 .h. The resulting expansion rate is close to 70% (Figure 2).
L'eau claire décantée, située en partie supérieure du réacteur au-dessus du lit de charbon actif (4), est récupérée par surverse avec une turbidité résiduelle inférieure à 1 NFU et une teneur en MES inférieure ou égale à 2 mg/1.The decanted clear water, located in the upper part of the reactor above the activated carbon bed (4), is recovered by overflow with a residual turbidity of less than 1 NFU and a MES content of less than or equal to 2 mg / l.
Exemple 2 :Example 2
Une installation selon la présente invention, comprenant un réacteur de traitement (1) contenant à son extrémité inférieure une zone aménagée (3) contenant un lit de graviers surmonté d'un lit de sable, dont la hauteur de garnissage est de 0,2 m.An installation according to the present invention, comprising a treatment reactor (1) containing at its lower end a developed zone (3) containing a bed of gravel surmounted by a bed of sand, the packing height of which is 0.2 m .
Au dessus de la zone aménagée (3), se trouve un lit de charbon actif (4) d'une hauteur de 0,7 m au repos. Le charbon actif introduit a une granulométrie de 0,1 à 0,4 mm. La concentration en charbon actif introduite est d'environ 380 g/1, lorsque le réacteur est à l'arrêt. Une telle installation est utilisée pour épurer de l'eau souterraine à une température comprise entre 14 et 16 °C. L'eau est injectée à la base du réacteur deAbove the developed area (3) is a bed of activated carbon (4) at a height of 0.7 m at rest. The active carbon introduced has a particle size of 0.1 to 0.4 mm. The activated carbon concentration introduced is about 380 g / l when the reactor is stopped. Such an installation is used to purify groundwater at a temperature between 14 and 16 ° C. Water is injected at the base of the reactor
1X O traitement (1) avec une vitesse ascensionnelle d'environ 10 m /m .h. Le taux d'expansion résultant est voisin de 200%. 1 XO treatment (1) with a rate of climb of about 10 m / m .h. The resulting expansion rate is around 200%.
L'eau claire décantée, située en partie supérieure du réacteur au-dessus du lit de charbon actif (4), est récupérée par surverse avec une turbidité résiduelle inférieure à 1 NFU et une teneur en MES inférieure ou égale à 2 mg/1. The decanted clear water, located in the upper part of the reactor above the activated carbon bed (4), is recovered by overflow with a residual turbidity of less than 1 NFU and a MES content of less than or equal to 2 mg / l.

Claims

REVENDICATIONS . CLAIMS.
1. Procédé de dépollution de fluide contenant des micropolluants organiques par adsorption sur charbon actif dans un réacteur de traitement à flux ascendant, comprenant l'injection du fluide à traiter en partie inférieure du réacteur contenant un lit de charbon actif de manière à créer une expansion dudit charbon en assurant parallèlement une séparation gravitaire entre les particules de charbon actif et le fluide, et la récupération par surverse du fluide décanté et dépollué situé en partie supérieure du réacteur surmontant le lit de charbon actif.1. A process for the depollution of fluid containing organic micropollutants by adsorption on activated carbon in an upflow treatment reactor, comprising injecting the fluid to be treated in the lower part of the reactor containing an activated carbon bed so as to create an expansion said coal in parallel providing a gravitational separation between the activated carbon particles and the fluid, and the overflow recovery of the decanted and de-polluted fluid located in the upper part of the reactor overlying the activated carbon bed.
2. Procédé selon la revendication 1, caractérisé en ce que le fluide à traiter est de l'eau, avantageusement de l'eau à potabiliser, en particulier de l'eau souterraine ou de l'eau de surface, telle que l'eau de rivière, l'eau de barrage, ou l'eau de nappe alluviale, ou de l'eau d'origine industrielle.2. Method according to claim 1, characterized in that the fluid to be treated is water, preferably water to drink, especially groundwater or surface water, such as water river, dam water, or alluvial water, or water of industrial origin.
3. Procédé selon la revendication 1 ou 2, caractérisé en ce qu'il ne nécessite l'ajout d'aucun autre additif de traitement à effet lestant de type coagulant et/ou floculant.3. Method according to claim 1 or 2, characterized in that it does not require the addition of any other coagulant-type and / or flocculant-type treatment additive.
4. Procédé selon l'une quelconque des revendications 1 à 3, caractérisé en ce que la granulométrie du charbon actif et la vitesse ascensionnelle du fluide sont choisies de manière à obtenir une suspension dense de charbon actif expansé sous forme de lit mobile, surmontée d'une hauteur de fluide clair décanté, la concentration moyenne en charbon actif étant avantageusement comprise entre 100 et 300 g/1 sur la hauteur du lit expansé, et inférieure à 2 mg/1 en partie supérieure de la zone de fluide clair surmontant le lit mobile de charbon actif.4. Method according to any one of claims 1 to 3, characterized in that the particle size of the activated carbon and the rate of rise of the fluid are chosen so as to obtain a dense suspension of activated carbon foamed in the form of a moving bed, surmounted by a clear fluid height decanted, the average concentration of activated carbon being advantageously between 100 and 300 g / l over the height of the expanded bed, and less than 2 mg / l in the upper part of the clear fluid zone surmounting the bed mobile activated carbon.
5. Procédé selon la revendication 4, caractérisé en ce que la granulométrie du charbon actif est comprise entre 100 et 800 μm, avantageusement entre 200 et 600 μm, et la vitesse ascensionnelle du fluide est comprise entre 2 et 20 m3/m2.h, avantageusement entre 8 et 15 m /m .h. 5. Method according to claim 4, characterized in that the particle size of the active carbon is between 100 and 800 microns, preferably between 200 and 600 microns, and the upward velocity of the fluid is between 2 and 20 m 3 / m 2 . h, advantageously between 8 and 15 m / m .h.
6. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce que le temps de contact du fluide avec le charbon actif est défini en fonction de la vitesse ascensionnelle du fluide et de la hauteur du lit de charbon expansé. 6. Method according to any one of the preceding claims, characterized in that the contact time of the fluid with the active carbon is defined as a function of the upward velocity of the fluid and the height of the expanded coal bed.
7. Procédé selon la revendication 6, caractérisé en ce que le temps de contact est compris entre 5 et 60 min, avantageusement entre 8 et 15 min.7. Method according to claim 6, characterized in that the contact time is between 5 and 60 min, preferably between 8 and 15 min.
8. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'au moins une partie du charbon actif est renouvelée périodiquement, par injection du charbon actif neuf dans le réacteur, avantageusement en partie inférieure du lit de charbon, et par extraction d'une quantité correspondante de charbon actif expansé.8. Method according to any one of the preceding claims, characterized in that at least a portion of the active carbon is renewed periodically, by injecting the new activated carbon into the reactor, preferably in the lower part of the coal bed, and by extraction. a corresponding amount of activated activated carbon.
9. Procédé selon l'une quelconque des revendications précédentes, caractérisé en ce qu'au moins une partie du charbon actif expansé extrait du réacteur est conditionnée dans au moins une cuve de stockage, avantageusement à des fins de recyclage après régénération partielle et/ou lavage.9. Process according to any one of the preceding claims, characterized in that at least a portion of the active activated carbon extracted from the reactor is conditioned in at least one storage tank, advantageously for recycling purposes after partial regeneration and / or washing.
10. Installation de dépollution de fluide contenant des micropolluants organiques comprenant au moins un réacteur de traitement (1) contenant :10. A fluid depollution installation containing organic micropollutants comprising at least one treatment reactor (1) containing:
- des moyens d'injection (2) du fluide à traiter, situés dans une zone aménagée (3) en partie inférieure du réacteur et surmontée d'un lit de charbon actif (4), un dispositif de récupération (5) du fluide clair décanté en partie supérieure du réacteur, des moyens d'injection (6) de charbon actif neuf ou régénéré, et des moyens d'extraction (7) de charbon actif expansé, et éventuellement au moins une cuve de stockage du charbon actif.- Injection means (2) for the fluid to be treated, located in a developed zone (3) in the lower part of the reactor and surmounted by a bed of activated carbon (4), a recovery device (5) clear fluid decanted in the upper part of the reactor, injection means (6) of activated carbon new or regenerated, and extraction means (7) of activated activated carbon, and optionally at least one storage tank of activated carbon.
11. Installation selon la revendication 10, caractérisée en que la zone aménagée (3) contient un lit bloquant, tel qu'un lit de graviers surmonté d'un lit de sable.11. Installation according to claim 10, characterized in that the fitted area (3) contains a blocking bed, such as a bed of gravel surmounted by a bed of sand.
12. Installation selon la revendication 10 ou 11, caractérisée en ce que le réacteur de traitement (1) et les moyens d'injection (2) du fluide sont agencés de manière à obtenir une vitesse ascensionnelle du fluide comprise entre 2 et 20 m /m .h, avantageusement entre 8 et 15 m3/m2.h, lorsque la granulométrie du charbon actif est comprise entre 100 et 800 μm, avantageusement entre 200 et 600 μm.12. Installation according to claim 10 or 11, characterized in that the treatment reactor (1) and the fluid injection means (2) are arranged to obtain a fluid upward velocity of between 2 and 20 m / m .h, advantageously between 8 and 15 m 3 / m 2 .h, when the particle size of the active carbon is between 100 and 800 microns, preferably between 200 and 600 microns.
13. Installation selon l'une quelconque des revendications 10 à 12, caractérisée en ce que le réacteur de traitement (1) est dimensionné en hauteur et en section de manière à obtenir une expansion du charbon actif comprise entre 20 et 300 %, avantageusement comprise entre 50 et 250 %, lorsque la vitesse ascensionnelle du fluide est comprise entre 2 et 20 m3/m2.h, avantageusement entre 8 et 15 m3/m2.h. 13. Installation according to any one of claims 10 to 12, characterized in that the treatment reactor (1) is dimensioned in height and in section so as to obtain an expansion of the active carbon of between 20 and 300%, advantageously included between 50 and 250%, when the upward velocity of the fluid is between 2 and 20 m 3 / m 2 .h, advantageously between 8 and 15 m 3 / m 2 .h.
PCT/FR2004/001735 2004-07-05 2004-07-05 Method for depolluting organic micropollutant-containing fluid by activated carbon absorption in a processing reactor WO2006013235A1 (en)

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB1428642A (en) * 1973-03-05 1976-03-17 Chiyoda Chem Eng Construct Co Method of treating water with active carbon

Non-Patent Citations (2)

* Cited by examiner, † Cited by third party
Title
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