KR100240377B1 - Reactor for the treatment of a liquid - Google Patents

Abstract

A reactor for treating liquid having a chamber containing an absorbent bed is provided. The inlet is located at the top of the chamber to introduce a given volume of liquid to be treated at regular intervals. The chamber also has an outlet located at the bottom for removing the treated liquid. The absorbent bed consists of a porous packing that can absorb the liquid introduced into the chamber into the capillary. At least one separating member is mounted horizontally in the chamber to divide the absorbent bed into at least two superimposed layers of defined height. This member is permeable to the liquid to be treated but is intended to cause one or more breaks in the capillaries in the chamber. The height of each layer is calculated as a function of the height that the liquid reaches by capillary action when liquid is supplied to a column filled with such continuous bed of absorbent bed. Such reactors are cheap to manufacture and use. The treatment time is easily adjustable by the capillary of the porous packing because of the presence of the separating member. Thus, the reactor can be used at maximum efficiency.

Description

Reactors for Liquid Processing

The present invention relates to a reactor for treating liquids.

"Reactor" means a device comprising a chamber in which a reaction is carried out between other elements. In this way, useful substances are produced or toxic substances are removed and thus no toxicity is lost.

Many industrial processes use reactors. Reactors, for example, are used in the petrochemical, pharmaceutical and food industries.

There are several types of reactors. However, most of the reactors can be divided into two basic categories called "batch reactors" on the one hand and "continuous reactors" on the other hand.

The choice of reactor is usually chosen as a function of the volume to be treated, the reaction kinetics, the nature of the reactants and the reaction conditions.

For batch reactors, one important property is the average time remaining. In use, a defined volume of liquid to be treated is introduced into the reactor and processed inside for a given time. During processing, the volume can react with the reactants and / or catalyst. The residence time is usually the same as the treatment time, ie the time during which the liquid reacts with the reactants and / or catalyst. The time is calculated as a function of the desired result. If the expected result is obtained, the treated liquid is removed from the reactor and charged with another volume of liquid to be treated.

In a batch reactor, other parameters are adjusted to obtain the required treatment. Among these parameters, the liquid treatment time in the reactor is the easiest to control. Usually the liquid to be treated in the batch reactor is kept in contact with the resin or reactant by agitation, bubbling or aeration steps that keep the resin or reactant uniform in suspension in the liquid.

The batch reactor has an outlet valve that is openable and closeable to remove liquid after treatment. According to the recent applicant's knowledge, no reactor uses a capillary tube as a means of retaining liquid in a porous packing.

It is an object of the present invention to provide a reactor for liquid treatment.

1 is a structural diagram of a reactor according to a preferred embodiment of the invention,

FIG. 2 is a structural representation of a packed column with a packing bed holding liquid in the capillary over height h, FIG.

FIG. 3 is a view similar to FIG. 2 showing the results obtained with the brake in the capillary;

4 is a graph showing the distribution of water mass held by capillaries in continuous and split columns,

5 is a structural diagram of a reactor of the present invention used for comparison purposes with a conventional batch reactor.

* Description of Major Symbols in Drawings *

2 ... reactor 4 ... chamber

6 ... absorption bed 8 ... separator

10 ... inlet 12 ... outlet

16 ... decantation pan 18 ... superimposed layer

30 ... dead space 50 ... ventilation system

The reactor according to the invention comprises a chamber, a liquid inlet, a liquid outlet, an absorbent bed and at least one separating member.

The chamber has a top and a bottom.

EMBODIMENT OF THE INVENTION Hereinafter, this invention is demonstrated in detail.

The inlet is located at the top of the chamber to introduce a given volume of liquid to be treated in the chamber at regular intervals. The outlet is located at the bottom of the chamber to remove the treated liquid therefrom.

The absorbent bed is mounted in the chamber between the upper and lower positions. The bed consists of a porous packing absorbable by capillary and thus holds the liquid introduced into the chamber for processing purposes. The porous packing can be reactive or non-reactive.

Each separating member extends horizontally in the chamber and divides the absorbent bed into at least two overlapping layers of a given height. This height is calculated as a function of the height of the liquid to be treated which is reached by capillary action when filling in a column packed with a continuous bed of absorbent bed. Each separating member is made of a material selected to be permeable to the liquid to be treated but also causes at least one break in the capillary in the chamber.

The residence and / or treatment time in the reactor according to the invention is as long as desired and easily adjustable. In practice, this corresponds to the time spent in the successive introduction of liquid into the chamber.

The reactor according to the invention uses capillaries of absorbent material to control the treatment time of the liquid to be treated. The liquid supplied into the chamber remains in the chamber unless another batch of liquid is introduced. Thus, if the time interval between two successive introductions of the liquid is sufficiently long compared to the filling time of the reactor, the chamber acts as a batch reactor. However, if the time between two successive introductions of the liquid is short, then the reactor operates as a continuous reactor.

Because of the separator divided by the absorption tube, the reactor can be used at maximum efficiency. In practice the separator defines the height of each bed layer to the maximum height at which the absorbing bed preserves the liquid by capillaries and thus removes any dead space in the chamber. If multiple separators are used to divide the absorber bed into layers, these layers may be filled continuously. In such a case the reactor according to the invention operates as a plurality of batch reactors operating sequentially.

For a given treatment, various types of porous packings can be used to maximize the yield of the reactor. The porous packing may or may not be reactive and is divided into two or more layers by one or more separating members.

For certain treatments, bacteria, catalysts, enzymes or antibodies are contacted or bound to the packing and are reactive. If the reaction rate is known to be delayed, the reactor according to the invention may be suitable for adjusting the residence time of the liquid therein and thus obtaining the required treatment.

The reactor according to the invention is not expensive at the time of manufacture and use. Therefore, it is particularly advantageous when the reactor manufacturing cost should be minimized.

In view of the prior art known to the applicant, it is known that any treatment performed by a capillary tube yields a very low yield, so using a reactor operated by a capillary tube is not advanced. The separating member used in the reactor according to the invention increases this yield and thus makes it possible to produce an efficient reactor.

Hereinafter, the present invention will be described in detail with reference to the accompanying drawings.

The reactor 2 according to the present invention is shown in FIG. The reactor 2 comprises an absorbent bed 6 divided into four layers by a chamber 4 having a top and a bottom, an inlet 10, an outlet 12 and three separators 8.

The inlet 10 is located at the top of the chamber 4. This inlet is used to introduce a fixed volume of liquid to be treated at regular intervals. The inlet 10 provides a distribution nozzle 14 to uniformly distribute the liquid to be treated at the top of the chamber. The outlet 12 is located at the bottom of the chamber 4. It is used to remove the treated liquid from the reactor.

The three separators 8 preferably consist of a grid which may consist of a plastic material, a metal or a resin, in particular polyvinyl chloride (PVC). Each grating is in the form of a mesh means having an opening small enough to create a hydraulic contact break and thus providing the brake needed in the capillary. The separator divides the absorbent bed into four overlapping layers 18 of equal height h _s . The absorbent bed consists of porous packing. The bed may be "uniform", meaning that the porous packing consists of a single piece. In addition, when the porous packing consists of multiple pieces, the bed may be "uneven". This is meaningful when the packing is non-uniform, because the capillary is made not only in the vertical axis but in all other directions. In this case, the liquid introduced into the chamber can move from one piece to another in the chamber without dropping between the pieces. A gas, such as air, is therefore also preferably introduced by another inlet located at the top of the chamber, which can be rotated in the chamber in an independent manner between packing pieces.

The porous packing may be reactive and may be combined with a reactant capable of reacting with at least one component of a solution of a microorganism such as a catalyst, protein, bacteria or a liquid to be treated. Preferably, the reactive porous packing is either natural or with nickel or platinum, activated carbon, zeolite, nonwovens with bacteria in contact with the fiber, polyacrylamide or alginate gels containing enzymes or antibodies and antibodies bound thereto. It may consist of metallic fibers coated with synthetic fibers.

Alternatively the porous packing may be non-reactive. In this case the packing preferably consists of polyurethane foam, polypropylene foam, glass fibers, peat moss, volcanic stone, papers, porous ceramics, natural or synthetic fibers or synthetic nonwovens.

In the preferred embodiment shown in FIG. 1, the reactor 2 also includes a decantation pan 16. It should be noted that the above-described distribution nozzle 14 as well as the inclined fan 16 is only a preferred embodiment of the present invention. All of these are not essential components for properly preparing the reactor 2.

2 and 3 show the capillary effect and the effect of the separator on the capillary. In FIG. 2, a capillary column consisting of a 1 mm diameter glass tube 20 comprising an upper end bed 24 and a lower end bed 26 is filled with a liquid such as water. To determine the height h _s at which the liquid is held by the capillary tube, excess liquid is introduced into the upper end bed 24 of the tube. After excess liquid flows downward, a fixed amount of liquid is maintained in the tube. The length between the upper and lower end beds of the liquid column is the capillary height h _s . The volume of liquid maintained in the column is referred to below as V _r .

The liquid does not completely fill the capillary if the height of the tube 20 is greater than h _s . In fact, as shown in Fig. 2, only a part of the tube corresponding to the height h _s is used. 3 shows a capillary tube 20 in which three layers superimposed in a discontinuous manner have the same height h _s . In order to use the capillary action of each tube in this way, a brake must be applied in the capillary tube. Such a break in the capillary is obtained by splitting. The brake in the capillary in the reactor according to the invention is obtained by a separator.

Like the splitting of the capillary, the splitting of the absorbent bed is split so that the capillary force is at its height, replacing the gravity on the smaller water column. In this way all absorbent beds of the column are used, while no separator is used, only the bottom of the column is actually used.

The curve shown in FIG. 4 shows the distribution of the mass of water held by the capillary tube as a function of height of the bed for continuous and split columns, or for both similar columns. On this curve, the height of the bed is recorded in abscissa and calculated as a function of the height of the column.

In FIG. 4, for a column divided into two 10 cm high fractions, the mass distribution of the liquid retained in the column is constant over their entire length, such that the fraction height of the column does not exceed the height hs. .

In the case of a continuous column, the bottom of the column contains the maximum amount of liquid, while there is no liquid or much less liquid at the top of the column.

The reactor 2 shown in FIG. 5 has been assembled in various specific dimensions and amounts as reported in the examples given below. The liquid to be treated enters the inlet 10 of the reactor and is internally distributed by the distribution nozzle 14. Liquid is filled through separator 8 and saturates the porous packing agent as absorbent bed 6. The reactor comprises three void spaces 30 which separate the absorber bed 6 into three layers. The void space 30 occurs because the chamber 4 of the reactor 2 used in this experiment is not specifically designed for this purpose but is substantially equivalent to one of the conventional reactors. In each layer of porous packing 6, the reactor includes a sampling valve 42 that can pick up a sample of liquid to evaluate the treatment. After processing, the liquid is removed from the chamber by an outlet provided with a drain valve 32. The drain valve is only applied arbitrarily because the capillary in the reactor of the present invention passively retains the liquid to be treated.

The reactor shown in FIG. 5 also has a recirculation pump 34 operated by an overflow pipe 38, an electric bowler 40 suitably connected to a timer, and a back flow. ventilation system 50 with conduct.

In fact, the reactor according to the invention shown in FIG. 5 is characterized by the volume D of the given liquid to be treated, the residence time t _res required to obtain the required treatment, the time t _inj required to load into the reactor, the surface area S of the reactor or capillary action. Due to the required type of packing, the density d _{1 of} the liquid to be treated and the number of required physical such as the height h _s at which the liquid reaches within the mass ratio R of the absorbent bed saturated with the liquid to be treated to the mass of the bed in dry form It is designed as a function of the property. The ratio R is a special characteristic of the porous packing used as the absorbent bed. The ratio has an apparent dry density d _app and can be measured on samples of absorbent beds of height lower than h _s .

As mentioned above, each absorbent bed has its own characteristics d _app , R and h _s . If these properties are not known, it is also possible to determine them experimentally. In order to determine R in the same column as shown in FIG. 2, the mass of the dry bed m ₀ occupies a height h _i much lower than the defined height h _s . After saturation with the liquid to be treated, the mass m ₁ of the same bed can be measured. Thus the ratio R can be determined by the equation:

Where m _l and mo are as defined above.

The density d _app can be calculated from the mass and its volume of the dry bed by the following equation:

Where s is the surface of the column used in the experiment and h _i , m _o and d _app are as described above.

The height h _s is determined by the equation:

Where h _s , _ml , s, d _app , R and h _i are as defined above. The values of R, d _app and h _s are constant depending on the absorption bed and are therefore independent of the type of reactor used.

The injection water n _inj into the volume D for a given treatment time t _d is calculated by the following equation:

Where n _inj , t _d , t _res and t _inj are as described above.

The volume Vr of the liquid to be treated contained in the reactor is calculated by the following equation:

Where V _r , D and n _inj are as defined above.

When seen the volume Vr of the liquid contained in the reactor, the volume V of the absorbent bed required to absorb the volume V _r of the liquid to be treated may be calculated by the following equation:

Where d ₁ is the density of the liquid to be treated and V, V _r , R and d _app are as defined above.

The mass M of the absorbent bed required for the proper operation of the reactor can be calculated by the following equation:

M = Vd _app

Where M, V and d _app are as defined above.

When the surface area S or height h _t of the reactor is known, the remaining of these two parameters can be calculated by the following equation:

Where S, V and h _t are as defined above.

Finally, the number of separators n _s needed in the reactor can be calculated by the following equation:

Where n _s , h _t and h _s are as defined above and the number n _s is rounded up immediately.

Hereinafter, the present invention will be described in more detail with reference to Examples.

Example

The reactor shown in FIG. 5 was assembled and used for domestic wastewater treatment. This reactor has the following characteristics:

Volume D of wastewater to be treated: 0.627 m 3;

Residence time t _res : 28 min;

Time required for introducing the liquid into the reactor t _inj : 0 minutes (can be ignored);

Height of absorbent bed h _t : 0.3 m;

Treatment time in volume D t _d : 1440 minutes (24 hours);

Density of waste water d ₁ : 1000 kg / m 3;

Porous packing: a piece of polyester nonwoven saturated with acrylic resin, 2.5 × 2.5 × 6 mm;

Height to reach the waste water by capillary action h _s: 0.112m;

Ratio R (mass of saturated bed to mass of dry bed): 4.52;

Density of dry bed d _app : 150 kg / m 3;

Using the values given above with the equations 4-8 and 10 given above, the following values were obtained:

(Equation 4 ')

(Equation 5)

㎥

㎥

(Equation 6 ')

㎥

㎥

(Equation 7 ')

M = Vd _app = 0,023.150 = 2.45kg

(Equation 8 ')

㎡

㎡

(Equation 10 ')

Thus, the assembled reactor has an absorption bed volume equal to 0.023 m 3 to maintain waste water of 0.012 m 3 and surface area of 0.077 m 2. It comprises two separators divided into three layers of absorbent beds each 0.1 m for a total height of about 0.3 m, and the height of the separator can be ignored.

Household wastewater is treated in the reactor for 28 minutes. Thus the reactor is filled 52 times a day (ie the load time of the reactor is negligible, ie t _inj = 0 min), since it operates 24 hours a day, 24 hours a day.

The table below shows the results of comparative administration of other parameters directly related to the purity of the wastewater. For comparison purposes, conventional reactors where packing was three times the reactor of the present invention were used. The surface area of the two reactors (the conventional percolation used for comparison purposes and the reactor according to the invention) was the same. As mentioned above, the reactor according to the present invention comprises an absorption bed divided into three layers (levels). In each bed, three levels, the outlet of the reactor, were measured.

parameter Septic Tank Penetration reactor, 200L / ㎡ / day Reactor according to the invention shown in Figure 5, 1800L / ㎡ / day Effluent Effluent Level 1 Level 2 Level 3 DBO ₃ 110 <5 6 5 <5 DBO ₃ -Sol - - <5 <5 <5 DCO 245 23 238 39 34 MES 35 3 5 5 <2 NTR 27.9 <0.5 37.2 24.3 14.4 NO ₂ -NO ₃ 0.86 50.6 0.64 13.3 19.6 Fecal content 29000 290 6900 1500 360

Filtrate effluent at all levels of the reactor according to the invention is demonstrated by a substantial reduction in fecal content.

It is also noted that, with the exception of some nitrogen-containing solutions (NTK), which are of secondary importance, there is no substantial difference between the results obtained at the outlet of a conventional infiltration reactor and the reactor according to the invention.

In order to better recognize the effluent of the reactor according to the present invention, the effluent volume of the septic tank was also measured. As can be seen, the reactor according to the present invention is much more effective than conventional septic tanks.

The superiority of the reactor according to the invention is in particular the amount of waste water the reactor can treat in one day and the amount of absorbent bed required to carry out a given treatment. Conventional permeation reactors used in the above-mentioned tests can treat 200 L / m 2 of filtration surface area per day with an absorbent bed volume of 0.07 m 3. The reactor according to the present invention shown in FIG. 5 can treat 1800 L / m2 of filtration area per day with an absorption bed volume of 0.023 m 3. Therefore, the reactor according to the present invention is capable of treating waste water 9 times or more than a conventional reactor having a volume three times larger. In other words, the reactor according to the present invention is about 27 times more efficient than conventional infiltration reactors. It is much more expensive as the reactor must be large in order to obtain the same excess in the permeation reactor.

According to the apparatus of the present invention described above, by mounting the separating member and using the capillary to induce one or more brakes in the chamber, the processing time can be easily adjusted and the efficiency can be maximized while reducing the dead space, manufacturing and use costs. have.

Claims (20)

A chamber having an upper portion and a lower portion; An inlet located at the top of the chamber to introduce a given volume of liquid to be treated within the chamber at regular intervals; An outlet for removing the treated liquid located at the bottom of the chamber; In the reactor for liquid treatment comprising: an absorption bed mounted in the chamber between the upper and lower positions, the absorption bed made of a porous packing capable of absorbing the liquid introduced into the chamber by a capillary tube, Further, the reactor, Having at least one separating member extending horizontally in the chamber to divide the absorbent bed into at least two superimposed layers of defined height, The height is calculated as a function of the height reached by capillary action when the liquid to be treated is fed into a column filled with a continuous bed of suction beds, Wherein said at least one separating member is permeable to the liquid to be treated but is selected to cause at least one brake on the capillary in the chamber The reactor of claim 1, wherein the at least one separating member consists of a grating having a mesh opening of a size small enough to produce a hydraulic contact break and thus a required brake in the capillary. The method of claim 1, wherein the porous packing of the absorbent bed is non-reactive, polyurethane foam, polypropylene foam, glass fiber, peat moss, volcanic stone, paper, porous ceramics, natural And a synthetic fiber and a synthetic nonwoven. 4. The reactor according to claim 3, wherein the at least one separating member is of a grating, having a mesh opening in the capillary with a mesh opening of a size small enough to form a hydraulic contact brake, and thus a brake required. The method of claim 1, wherein the porous packing of the absorbent bed is a reactive, non-woven fabric with a catalyst, activated carbon, zeolite, bacteria adhering to the fiber, polyacrylamide or an alginate gel and enzyme containing an enzyme or antibody Reactor characterized in that it is selected from the group consisting of combined natural fibers and synthetic fibers 6. The reactor according to claim 5, wherein the at least one separating member consists of a grating having a hydraulic contact brake, and thus a mesh opening of a size small enough to produce the required brake. The method according to claim 1, wherein the injection water n _inj of the liquid in the chamber, the volume V _r of the liquid contained in the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the surface area S of the reactor and the number n _s of the separating member are Volume D of liquid to be treated during treatment time t _d , residence time t _res required to obtain the required treatment, loading time t _{inj of} reactor, height h _s reached by liquid by capillary action in the column, absorption into reactor Reactor as a function of the height h _t of the bed and the mass ratio R of the absorbent bed saturated with liquid to be treated to the mass of the bed in dry form, selected according to The dry bed has an apparent density d _app : Equation 4

Provided that n _inj , t _d , t _res and t _inj are as described above; Equation 5

Provided that Vr, D and n _inj are as defined above; Equation 6

Provided that d ₁ is the density of the liquid to be treated and V, Vr, R and d _app are as defined above; Equation 7 M = Vd _app Provided that M, V and d _app are as defined above; Equation 9 h _t =

Provided that S, V and h _t are as defined above; Equation 10 n _s =

With the proviso that n _s , h _t and h _s are as defined above and the number n _s is rounded up. The method according to claim 3, wherein the injection water n _inj of the liquid in the chamber, the volume V _r of the liquid contained in the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the surface area S of the reactor, and the number n _s of the separating member are Volume D of liquid to be treated during treatment time t _d , the residence time t _res required to obtain the required treatment t, the loading time of the reactor t _inj , the height of the liquid reaching by capillary action in the column h _s , absorbed into the reactor A reactor characterized by the following formula as a function of the height h _t of the bed and the mass ratio R of the absorbent bed saturated with liquid to be treated with respect to the mass of the bed in dry form: The dry bed has an apparent density d _app : Equation 4

Provided that n _inj , t _d , t _res and t _inj are as described above; Equation 5

Provided that Vr, D and n _inj are as defined above; Equation 6

Provided that d ₁ is the density of the liquid to be treated and V, Vr, R and d _app are as defined above; Equation 7 M = Vd _app Provided that M, V and d _app are as defined above; Equation 9 h _t =

Provided that S, V and h _t are as defined above; Equation 10 n _s =

With the proviso that n _s , h _t and h _s are as defined above and the number n _s is rounded up. The method according to claim 5, wherein the injection water n _inj of the liquid in the chamber, the volume V _r of the liquid contained in the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the surface area S of the reactor and the number n _s of the separating member are treatment time t _d height of the liquid is reached by capillary action into the loading time t _inj, the column of the remaining time t _res, the reactor required to achieve a process of a volume D, necessary for the liquid to be treated for a h _s, absorbed in the reactor bed Reactor according to the following formula as a function of the height h _t and the mass ratio R of the liquid-saturated absorbent bed to be treated with respect to the mass of the bed in dry form: The dry bed has an apparent density d _app : Equation 4

Provided that n _inj , t _d , t _res and t _inj are as described above; Equation 5

Provided that Vr, D and n _inj are as defined above; Equation 6

Provided that d ₁ is the density of the liquid to be treated and V, V _r , R and d _app are as defined above; Equation 7 M = Vd _app Provided that M, V and d _app are as defined above; Equation 8 S =

Provided that S, V and h _t are as defined above; Equation 10 n _s =

With the proviso that n _s , h _t and h _s are as defined above and the number n _s is rounded up. The method according to claim 1, wherein the injection water n _inj of the liquid in the chamber, the volume V _r of the liquid contained in the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the height h _t of the absorbent bed in the reactor, and The number n _s is the volume D of the liquid to be treated during the treatment time t _d , the residence time t _res required to obtain the required treatment, the loading time t _{inj of the} reactor, the height h _s reaching the liquid by capillary action in the column, A reactor characterized by the following equation as a function of the surface area S of the reactor and the mass ratio R of the absorbent bed saturated with liquid to be treated with respect to the mass of the bed in dry form: The dry bed has an apparent density d _app : Equation 4

Provided that n _inj , t _d , t _res and t _inj are as described above; Equation 5

Provided that V _r , D and n _inj are as defined above; Equation 6

Provided that d ₁ is the density of the liquid to be treated and V, V _r , R and d _app are as defined above; Equation 7 M = Vd _app Provided that M, V and d _app are as defined above; Equation 9 h _t =

Provided that S, V and h _t are as defined above; Equation 10 n _s =

Provided that n _s , h _t and h _s are as defined above and the number n _s is rounded up immediately. The method of claim 3, wherein the height h _t and separating members of the absorbent bed in the volume of liquid V _r, the mass of the volume V, absorbent bed of the absorbent bed M, the reactor contained in the water injection of liquid n _inj, the reactor in the chamber The number n _s is the volume D of the liquid to be treated during the treatment time t _d , the residence time t _res required to obtain the required treatment t, the loading time of the reactor t _inj , the height h _s that the liquid reaches by capillary action in the column, A reactor characterized by the following equation as a function of the surface area S of the reactor and the mass ratio R of the absorbent bed saturated with liquid to be treated with respect to the mass of the bed in dry form The dry bed has an apparent density d _app : Equation 4

Provided that n _inj , td, t _res and t _inj are as described above; Equation 5

Provided that Vr, D and n _inj are as defined above; Equation 6

Provided that d ₁ is the density of the liquid to be treated and V, V _r , R and d _app are as defined above; Equation 7 M = Vd _app Provided that M, V and d _app are as defined above; Equation 9 h _t =

Provided that S, V and h _t are as defined above; Equation 10 n _s =

With the proviso that n _s , h _t and h _s are as defined above and the number n _s is rounded up. The method according to claim 5, wherein the injection water n _inj of the liquid in the chamber, the volume V _r of the liquid contained in the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the height h _t of the absorbent bed in the reactor, The number n _s is the volume D of the liquid to be treated during treatment time t _d , the residence time t _res required to obtain the required treatment, the loading time t _{inj of the} reactor, the height h _{s the} liquid reaches by capillary action in the column, the reactor Reactor characterized in that it is selected by the following formula as a function of the surface area S and the mass ratio R of the liquid The dry bed has an apparent density d _app : Equation 4

Provided that n _inj , t _d , t _res and t _inj are as described above; Equation 5

Provided that Vr, D and n _inj are as defined above; Equation 6

Provided that d ₁ is the density of the liquid to be treated and V, V _r , R and d _{app are} as defined above; Equation 7 M = Vd _app Provided that M, V and d _app are as defined above; Equation 9 h _t =

Provided that S, V and h _t are as defined above; Equation 10 n _s =

With the proviso that n _s , h _t and h _s are as defined above and the number n _s is rounded up. The reactor of claim 1, comprising one or more other inlets located at the top of the chamber for introducing air therein. The reactor of claim 3, comprising one or more other inlets located at the top of the chamber for introducing air therein. 8. A reactor according to claim 7, comprising one or more other inlets located at the top of the chamber for introducing air therein. 9. The reactor of claim 8 comprising at least one other inlet located at the top of the chamber for introducing air therein. 10. The reactor of claim 9, comprising one or more other inlets located at the top of the chamber for introducing air therein. 11. The reactor of Claim 10, comprising one or more other inlets located at the top of the chamber for introducing air therein. 12. The reactor of claim 11, comprising one or more other inlets located at the top of the chamber for introducing air therein. 13. The reactor of Claim 12, comprising one or more other inlets located at the top of the chamber for introducing air therein.

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