MXPA97001741A - Reactor for the treatment of a liquid - Google Patents

Abstract

A reactor for the treatment of a liquid, having a chamber containing an absorbent bed. An entrance is located in the upper portion of the chamber to introduce at regular intervals a given volume of the liquid to be treated. The chamber also has an outlet located in its lower portion to remove the treated liquid. The absorbent bed consists of a porous packing capable of absorbing by capillarity a liquid introduced into the chamber. At least one spacing member that is mounted horizontally within the chamber in order to divide the absorbent bed into at least two superimposed layers of a given height. This member is permeable to the liquid that will be treated but is designed to cause at least a break in the capillarity within the chamber. The height of each layer is calculated as a function of the height reached by the liquid capillary action, when fed into a column filled with a continuous layer of the same absorbent bed. This reactor is not of expensive manufacture and use. The treatment time is easily controllable with the capillarity of the porous packaging and thanks to the presence of the separation members. Therefore, the reactor can be used with maximum efficiency

Description

REACTOR FOR THE TREATMENT OF A LIQUID FIELD OF THE INVENTION The present invention relates to a reactor for the treatment of a liquid.

DESCRIPTION OF THE PREVIOUS TECHNIQUE "Reactor" is understood as a device that includes a chamber in which a reaction between different elements takes place. In this way, useful substances are created or noxious substances are destroyed, thus losing their harmful nature. Numerous industrial processes make use of reactors. For example, reactors are used in the petrochemical, pharmaceutical and food industries. There are several types of reactors. However, most reactors can be divided into two basic categories, which include, on the one hand, the so-called "batch reactors" and, on the other hand, the so-called "continuous reactors". The selection of a reactor is normally carried out as a function of the volume to be treated, the reaction kinetics, the nature of the reactors and the reaction conditions. For a batch reactor, one of the important characteristics is the average residence time. During use, a given volume of the liquid to be treated is introduced into the reactor and treated therein for a given period of time. During the treatment, this volume can react with a reagent and / or catalyst. The residence time is normally equal to the treatment time, ie the time during which the liquid can react with the reagent and / or the catalyst. This time is calculated as a function of the desired result. When the expected result is obtained, the treated liquid is removed from the reactor to make room for another volume of liquid to be treated. In a batch reactor, different parameters can be adjusted to obtain the required treatment. Among these parameters, the treatment time of the liquid inside the reactor is the easiest to control. Normally, the liquid to be treated in the batch reactor is kept in contact with a resin or with a reagent by means of a stirring, bubbling or aerating step which allows the resin or the reagent to be kept uniformly suspended in the liquid. Batch reactors are usually provided with an outlet valve that can be opened to remove the liquid after treatment. Currently, as far as the applicant is aware, there is no lo-1 '/ MX reactor that uses capillarity as a means to retain the liquid within the porous package.

OBJECTIVE AND SUMMARY OF THE INVENTION The object of the present invention is to provide a reactor for the treatment of a liquid. The reactor according to the invention comprises a chamber, a liquid inlet, a liquid outlet, an absorbent bed and, at least, a separation member. The chamber is provided with an upper portion and a lower portion. The entrance is located in the upper portion of the chamber to introduce, within the chamber, at regular intervals, a given volume of the liquid to be treated. The outlet is located in the lower portion of the chamber to remove the treated liquid from it. The absorbent bed is mounted within the chamber between the upper and lower portions thereof. This bed consists of a porous packing capable of absorbing by capillarity and, in this way, retaining the liquid introduced into the chamber for treatment purposes. The porous packaging can be reactive or non-reactive. Each spacing member extends horizontally within the chamber and divides the absorbent bed into at least two superimposed ones of a given height. This height is calculated as a function of the height of the liquid to be treated, which is reached by the action of capillarity when it is filled in a column filled with a continuous layer of the same absorbent bed. Each separation member is made of a material that is selected to be permeable to the liquid to be treated but also to cause at least a break in the capillarity within the chamber. The residence and / or treatment time within the reactor according to the invention can be as long as desired and easily controllable. Of course, corresponds to the time elapsed between two successive introductions of liquid inside the chamber. The reactor according to the invention makes use of the capillarity of the absorbent material to control the treatment time of the liquid to be treated. The liquid fed into the chamber remains inside it as long as another liquid charge is not introduced. Thus, if the time interval between two successive introductions of the liguid is sufficiently long compared to the filling time of the reactor, the latter will operate as a batch reactor. However, if the time between two successive introductions of liquid is short, the reactor will then operate as a continuous reactor. Thanks to the separators that divide the absorbent bed, the reactor can be used with maximum efficiency. Of course, the spacers limit the height of each layer of the bed to the maximum height at which the absorbent bed can retain the liquid by capillary action, thereby eliminating any dead space within the chamber. In the case where several separators are used to divide the absorbent bed into layers, these layers can be filled successively. In each case, the reactor according to the invention operates as a plurality of batch reactors operating in sequence. In order to maximize the performance of the reactor for a given treatment, various types of porous packaging can be used. The porous packaging can be reactive or not and can be separated into two or more layers by one or more separation members. For specific treatments, bacteria, catalysts, enzymes or antibodies can be added or grafted to the packaging to make it reactive. When it is known that the reaction rate is slow, the reactor according to the invention can be adapted to adjust the residence time of the liquid in it and thus obtain ; ::: < .-C > / MX the required treatment. The reactor according to the invention is not expensive to manufacture. Therefore, it is particularly advantageous when the construction costs of the reactor should be minimized. In view of the prior art known to the Applicant, it was not obvious to use a reactor that operates by capillary action because it is known that any treatment effected by capillarity provides very low performance. The separation members used in the reactor according to the invention allow this yield to be increased and thus make the reactor as efficient as any other.

BRIEF DESCRIPTION OF THE DRAWINGS The invention will be better understood by reading the following non-restrictive description of a preferred embodiment thereof, made with reference to the accompanying drawings, in which: Figure 1 is a schematic representation of a reactor according to a preferred embodiment of the invention. Figure 2 is a schematic representation of a column filled with packing bed which retains a liquid by capillarity at a height hs; i ..: O - ') / M Figure 3 is a view similar to that of Figure 2, showing the result obtained with a break in capillarity; Figure 4 is a curve illustrating the distribution of water mass supported by capillarity within a continuous column and a segmented column; and Figure 5 is a schematic representation of a reactor according to the invention that was used for comparison purposes against a conventional batch reactor. For reasons of simplicity, the same reference numbers have been used to identify the same structural elements in the following description and in the accompanying drawings.

DESCRIPTION OF A PREFERRED MODE OF THE INVENTION A reactor (2) according to the invention is shown in Figure 1. This reactor (2) comprises a chamber (4) having an upper portion and a lower portion, an entrance (10). ), an outlet (12) and an absorbent bed (6) divided into four layers by means of three separators (8). The entrance (10) is located in the upper portion of the chamber (4). This input is used to enter a given volume of liquid at regular intervals to be treated. The inlet (10) is provided with a dispensing nozzle (14) to distribute evenly to the liquid to be treated in the upper portion of the chamber. The outlet (12) is located in the lower portion of the chamber (4). It is used to remove the treated liquefied from the reactor. The three separators (8) preferably consist of grids that can be made of plastic material, metal or resin, especially polyvinyl chloride (PVC) each grid has the shape of a mesh provided with openings small enough to create a hydraulic contact break and , in accordance with the above, the required rupture in the capillarity. The separators divide the absorbent bed into four superposed layers (18) of the same height hs. The absorbent bed consists of a porous packing. The bed can be "homogeneous", which means that the porous packing consists of a single piece. Alternatively, the bed may be "heterogeneous" when the porous packing consists of several pieces. It is worth mentioning that when the packaging is heterogeneous, the capillarity is obtained not only on the vertical axis, but also in all other directions. In this case, the liquid that is introduced into the chamber can move from one piece to another inside the chamber, without dripping between the pieces. Thus, it is possible to introduce a gas such as air through another entrance, preferably also located in the upper portion of the chamber, and to cause this gas to circulate inside the chamber independently between the pieces of the package. The porous packaging can be reactive and be coupled with a catalyst, proteins, microorganisms such as batteries or a reagent which can react with at least one of the components of the solution of the liquid to be treated. Preferably, the reactive porous pack may consist of metal fibers covered by a catalyst of the niguel or platinum type, activated carbon, zeolites, nonwovens having bacteria adhered to their fibers, polyacrylamides or alginate gels containing enzymes or antibodies and natural fibers or synthetics which have antibodies grafted thereto. Alternatively, the porous pack may be non-reactive. In this case, this pack preferably consists of polyurethane foams, polypropylene foams, glass fibers, peat moss, volcanic rock, paper, porous ceramics, natural or synthetic fibers or synthetic non-woven fabrics. In the preferred embodiment shown in Figure 1, the reactor (2) also comprises a settling tank - t / MX (16). It is worth mentioning that the decantation tank (16) as well as the distribution boom (14) mentioned above, are only preferred embodiments of the invention. These two are not essential for proper preparation of the reactor (2). Figures 2 and 3 illustrate the capillary effect and the influence of the separators on capillarity. In Figure 2, a capillary column consisting of a glass tube (20) of 1 mm in diameter comprising an upper end (24) and a lower end (26) is filled with a liquid, such as water. In order to determine the height to which the liquid is required by capillarity, an excess amount of the liquid is introduced into the upper end (24) of the tube. After the excess of the liquid has flowed down, a given amount of the liquid is retained within the tube. The distance between the upper and lower ends of this column of height is the capillarity height hs. The volume of the retentate retained in the column is hereinafter referred to as Vr. The liguid does not completely fill the capillary tube if the height of the tube (20) is greater than hs. In fact, as shown in Figure 2, only a portion of the tube corresponding to the height hs is used. Figure 3 illustrates three capillary tubes (20) of the same height hs, i: i: ..- '!' HX which are superimposed in discontinuous form. To do so and use the action by capillarity of each tube, a break in capillarity must be achieved. This rupture in capillarity is obtained by segmentation. In the reactor according to the invention, the capillary rupture is achieved by the separators. The separation of the absorbent bed, such as the segmentation of the capillary tube, allows the force of capillarity to annul the gravitational force that is exerted on the water column which has a more sticky height due to which it is segmented. In this way, the entire absorbent bed of the column is used, whereas, when a separator is not used, only the lower portion of the column is actually used. The curve shown in Figure 4 illustrates the distributions of the water mass retained by capillarity as a function of the bed height, in the case of a continuous column and in the case of a segmented column, otherwise, both columns would be Similar. In this curve, the height of the bed is reported in the abscissa and is calculated as a function of the height of the column. In the view of Figure 4, it is obvious that for the column segmented into two portions of 10 cm in height, the distribution of the mass of retained liguid within the column is constant over the entire length of the column.

This is achieved because the height of the column segment does not exceed the height h.In the case of the continuous column, the lower portion of the column contains a maximum amount of The reactor (2) shown in Figure 5 was constructed with the various dimensions and specific capabilities reported in the example given below.The liguid that will be treated was brought to the entrance (Fig. 10) of the reactor and distributed therein by means of a distribution nozzle 14. The liquid passed through the separators 8 and impregnated and saturated a porous package that acts as an absorbent bed 6. three dead spaces (30) separating the absorbent bed (6) in three layers The dead spaces (30) were there because the chamber (4) of the reactor (2), which is used for the experiment, was not designed specifically for this purpose, but they really corresponded to those of a conventional reactor. Under each layer of porous pack (6), the reactor comprised a sampling valve (42) that allowed to collect samples of the liquid in order to evaluate the treatment. After being treated, the liguid was removed from the chamber by an outlet provided with a drain valve (32). Again, It is worth mentioning that this drainage valve is only optional, since in the reactor according to the invention, capillary action allows to retain in a passive form the liquid to be treated. The reactor shown in Figure 5 also comprised a ventilation system (50) provided with a spill tube (38), a recirculation pump (34) operated by an electric motor (40) which was preferably connected to a timer and, a counterflow conduit (48). In practice, the reactor according to the invention as shown in Figure 5 was constructed as a function of a plurality of physical characteristics required, such as a given volume D of the temperature to be treated, the residence time t, e ? It is necessary to obtain the necessary treatment, the time needed to charge the reactor, the surface S of this reactor or the height reached by the liquid due to the capillary action within a given type of packing. The density x of the liquid to be treated and the ratio R of the mass of the absorbent bed saturated with the liquid will be treated with respect to the mass of the same bed in dry form. The ratio R is a characteristic that is specific- for the porous bundle used as an absorbent bed. This relationship can be measured in an absorbent bed sample of a height below hs, which has an apparent dry density of dapp. As previously indicated, each absorbent bed has its own characteristics (dapp, R and hs). If these characteristics are not known, it is possible to determine them experimentally. To determine R, one can, in a column identical to that shown in Figure 2, determine the mass of the dry bed as it occupies a height h? much smaller than the supposed height hs. After saturation with the liguid that will be treated, the mass t x of the same bed can be measured. Thus, one can determine the relation R in accordance with the equation: ÍI1 o where v 1 and m0 are as defined above. The density dapp, can be calculated from the mass of the dry bed and its volume, according to the equation: m d = -2_,, app s. j (2) where s is the surface of the column that is used for experimentation and h¿, trio and dapp are as defined above.

The height hs is determined in accordance with 1 < equation: where hs, va1, s, dapp, R and h are as defined above. It is worth mentioning that the values of R dapp and hs are specific for the absorbent bed and, accordingly, independent of the type of reactor that will be used. The injection number n? Nj during a given period of treatment t (J of a volume D is calculated according to the equation: where n? n], t, three and t? n-, are as defined above. The volume Vr of the liquid that will be treated inside the reactor is calculated according to the equation: v_ = n D in i (5) where Vr, D and n nj are as defined above. When one knows the volume Vr of the content contained in the reactor, the volume V of the absorbent bed I. • -l! MX necessary to absorb the volume Vr of the liquid that will be treated, can be calculated by means of the following equation: v = *. (? -l) .d app (6) where dx is the density of the liquid that will be treated and, V, Vr, R and dapp are as defined above. The mass of the absorbent bed necessary for proper operation of the reactor can be calculated by the following equation: w = v. dpp (7) where M, V and dj are as defined above. Depending on whether the surface S or the height ht of the reactor is known, the other of these two parameters can be calculated by the following equation: t (8) or, _ V! ^ ~ 'S (9) where S, V and ht are as defined above. Finally, the number ns of spacers required inside the reactor can be calculated according to the equation: i / MX where ns, hc and hs are as defined above and the ns number is rounded to the next higher data.

EXAMPLE The reactor shown in Figure 5 was constructed and used to treat domestic wastewater. This reactor had the following characteristics: volume D of wastewater to be treated: 0. 627 m3; - residence time three: 28 minutes - time needed for the introduction 0 minutes of the temperature within the reactor: (negligible), • - height ht of the absorbent bed: 0.3 meters; - treatment time cj of volume D: 1440 minutes (24 hours); density d ^ of waste water: 1000 kg / m; porous bundle: fragments of nonwoven polyester fabric of 2.5 X 2.5 X 6 mm, saturated with acrylic resin; - height he. reached by the residual water by 0.112 meters capillary action: - R ratio (mass of the saturated bed to the mass of the dry bed): 4.52; density of dapp of the dry bed: 150 kg / m; i:.: »/ X Using the values provided above and the equations 4 to 8 and 10 provided above, one can obtain: ? Í = I d app = 0, '023, 150 = 2, 5kg (7') ? r 0.3. { 8 ') h '_ 0.3"*? ~ 1 = 0, 112 2 (10') Therefore, the reactor that was built had an absorbent bed volume equal to 0.023m making it possible to retain 0.012 m of residual water and a surface of 0.077 m. It comprised 2 separators that divide the absorbent bed in three layers of 0.1 meter each, for a total height equal to approximately 0.3 meters, keeping in mind that the height of the separators was negligible. The domestic wastewater was treated for 28 minutes inside the reactor. In this way, in order to : -; io- ^ 7M >; operating non-stop for 24 hours a day, the reactor was filled 52 times a day (considering that the loading time of the reactor was negligible, viz. t nj = 0 minutes). The following table shows the result of comparative dosages of different parameters directly related to the purity of the wastewater. For comparison purposes, a conventional reactor having a package of a volume three times larger than that of the reactor, according to the invention, was used. The surfaces of both reactors were identical (the conventional percolation reactor used for comparison purposes and the reactor according to the invention). As mentioned, the reactor according to the invention comprised an absorbent bed divided into three layers (or levels). A measurement was made under each layer, level 3 is that of the reactor outlet.

V7MX It is worth mentioning that the filtering efficiency of each level of the reactor according to the invention is evidenced by the substantial reduction in the amount of fecal content. It is also worth noting that there is no substantial difference between the results obtained with the conventional percolation reactor and those obtained at the output of the reactor in accordance with the reaction, except for some compounds containing secondary importance hydrogen (NTK). In both cases, the quality of wastewater treatment was excellent. In order to better appreciate the efficiency of In the reactor according to the invention, measurements were also made in the effluent of a septic tank. As can be seen, the reactor according to the invention is much more efficient than a conventional septic tank. The superiority of the reactor according to the invention resides, in particular, in the amount of waste water that the reactor can treat per day and the amount of absorbent bed required to effect a given treatment. The conventional percolation reactor used in the aforementioned test could treat 200 liters per square meter of filtering surface per day, with an absorbent bed volume of 0.07 m '. The reactor according to the invention as shown in Figure 5, could treat 1800 liters per square meter of filtering surface per day with an absorbent bed volume of 0.023 m. Thus, it is obvious that the reactor according to the invention can treat up to S times more waste water than a conventional reactor having a volume three times as large. In other words, the reactor according to the invention is about 27 times more efficient than a conventional reactor by percolation. In order to obtain the same outflow in a reactor by percolation, this reactor must be much larger and, therefore, much more expensive. It is worth mentioning that numerous modifications could be made to the present invention without deviating from the scope thereof, as defined in the appended claims.

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Claims (2)

1. NOVELTY OF THE INVENTION Having described the present invention, it is considered as a novelty and, therefore, the content of the following CLAIMS is claimed as property; 1. In a reactor for the treatment of a liquid, the reactor comprises: a chamber provided with an upper portion and a lower portion; - an entrance located in the upper portion of the chamber to introduce at regular intervals a given volume of the liquid to be treated inside the chamber, - an outlet located in the lower portion of the chamber to remove the treated liquid from it; and an absorbent bed mounted inside the chamber, between the upper and lower portions thereof, the bed consists of a porous packing capable of absorbing by capillarity the liquid introduced into the chamber; the improvement wherein the reactor further comprises: at least one spacing member extending horizontally within the chamber in order to divide the absorbent bed into at least two superimposed ones of a given height, the height is calculated as a function of the height that the liquid will be treated ! .- - MX reaches by capillary action when fed in a column filled with a continuous layer of the same absorbent bed, at least one separation member is selected to be permeable to the liquid to be treated, but to cause less a break in capillarity inside the camera. 2. The improved reactor according to claim 1, characterized in that the at least one separating member consists of a grating which has mesh openings of a size that is small enough to create a hydraulic contact break, and, in accordance with this, the required break in the length. 3. The improved reactor was? claim 1, characterized in that the porous packing of the absorbent bed is non-reactive and is selected from the group consisting of polyurethane foams, polypropylene foams, glass fibers, moss peat, volcanic rock, paper, porous ceramics, fibers natural and synthetic and non-woven synthetic genera.
2. 2. The improved reactor according to the claim 3, characterized in that the at least one separating member consists of a grid having mesh openings of a size that is sufficiently glued to create a hydraulic contact break and, accordingly, the required break in capillarity. '/ MX 5. The improved reactor according to claim 1, characterized in that the porous packing of the absorbent bed is reactive and is selected from the group consisting of metal fibers covered by a catalyst, activated carbon, zeolites, nonwovens having bacteria adhered to their fibers, polyacrylamide or alginate gels that contain enzymes or antibodies and, natural or synthetic fibers that have antibodies inserted therein. 6. The improved reactor according to the claim 5, characterized in that the at least one separating member consists of a grid having mesh openings of a size which is sufficiently glued to create a rupture of hydraulic contact and, accordingly, the required break in capillarity. 7. The improved reactor according to claim 1, characterized by the number of liquid injection njnj into the chamber, the volume Vr of the liquid contained within the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the S surface of the reactor and the number ns of separation members are selected as a function of the volume D of the liquid which will be treated during the treatment period t¿, the residence time three which will be regulated to obtain the required treatment, the time of Tinj reactor charge, The height hs reached by the liquid per capillary action in the column, the height ht of the absorbent bed in the reactor and the ratio R of the bed mass in dry form, the dry bed has a apparent density dapp, using the following equations: (t + t, ") (4) in which n ^ nj, t¿, three and tinj, are as defined above, in which Vr, D and ninj are as defined above, in the gue di del líguido that will be treated, V, Vr, R and dapp are as defined above, "= V.dapp < 7 > in which M, V, and dapp are as defined above, ^ ~ S (9) in which S, V and ht are as defined above, n = ~ -l s h (10) -'I'ÍM? in which ns, ht and hs are as defined above and where the number ns is rounded to the next higher integer. 8. The improved reactor according to claim 3, characterized by the ninj injection number of the liquid inside the chamber, the volume Vr of the contained content within the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the surface S of the reactor and the number ns of the separation members are selected as a function of the volume D of the liquid that will be treated during a treatment period t¿, the tree residence time that is regulated to obtain the required treatment, the time of treatment. load of the reactor tinj, the height hs reached by the liquid by capillary action in the column, the height ht of the absorbent bed in the reactor and the ratio R of the mass of the absorbent bed saturated with lguid that will be treated to the mass of the same bed in dry form, the dry bed has an apparent dapp density, using the following equations: in gue nnj, t¿, three and t_nj, they are as defined above, D V 'i nj (5) - 'MX in which Vx, d and n? R are as defined above, (R ~ l) .dapp < 6 > in gue di is the density of the liquid to be treated, V, Vr, R and dapp are as defined above, w = v.dapp < 7 > in which M, V and dapp are as defined above, in which S, V and ht are as defined above, in which gs ns, ht and h are as defined above-and where the number n is rounded to the next higher integer. 9. The improved reactor according to claim 5, characterized by the number of injection of in-liguid ink into the chamber, the volume Vr of the contained content within the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the surface S of the reactor and the number ns of the separation members are selected as a function of the volume D of the liquid which will be treated during a treatment period t ^, the residence time three which is regulated to obtain the required treatment, the time of load of the reactor tj.nj, the height hs reached by the liquid by capillary action in the column, the height ht of the absorbent bed in the reactor and the ratio R of the mass of absorbent bed saturated with liquid that will be treated to the mass of the same bed in dry form, the dry bed has an apparent dapp density, using the following equations: where _n-,, t ^, three and t n, are as defined above, t »t (5) where Vx, D and n-n? they are as defined above, where di is the density of the liquid to be treated, V, Vr, R and dapp are as defined above, M = V "d app (?) where M, V and dapp are as defined above, \ ~ S (9) where S, V and ht are as defined above, 'MX where ns, ht and hs are as defined above and where the number ns is rounded to the next higher integer. 10. The improved reactor according to the claim 1, characterized in that the injection number n? Nj of liquid inside the chamber, the volume Vr of liquid contained within the reactor, the volume V of the absorbent bed, the mass M of the absorbent bed, the height ht? The absorbent bed in the reactor and the number ns of the separation members are selected as a function of the volume D of the liquid that will be treated during the period of treatment, the residence time three that is required to obtain the required treatment, time? e load of the reactor tinj, the height hs reached by the liquid by capillary action in the column, the surface S? the reactor and the ratio R of the mass of the absorbent bed saturated with the liquid that will be treated to the mass of the same bed in dry form, the dry bed has an apparent dapp density, using the following equations: nin (ttas + ti, / ij.) (4) where n.¡_nj, t¿, three and tinj, are as defined above, v -. in which Vr, D and n nj are as defined above, where dx of the liquid to be treated, V, Vr, R and dapF are as defined above, w = v.dßpp (7) in which M, V and dapp are as defined above, "i S (9) where S, V and ht are as defined: aron previously, in which ns, ht and hs are as previously stated and where the number ns is rounded to the next higher integer. 11. The improved reactor according to the claim 3, characterized in that the liquid ejection number ninj within the chamber, the volume Vr of liquid contained within the reactor, the volume V of the absorbent bed, the mass of the absorbent bed, the height ht of the absorbent bed in the reactor and the number ns of the -QTMX separation members are selected as a function of the volume D of the liquid that will be treated during the treatment period t¿, the residence time three that is required to obtain the required treatment, the loading time of the tinj reactor, the height hs reached by the liquid by capillary action in the column, the surface S of the reactor and the ratio R of the mass of the saturated absorbent bed with the liquid that will be treated to the mass of the same bed in dry form, the dry bed has a density Apparent dapp, using the following equations: inj (t + t.) (4) er. What nj n j, td, t? and t? r. , they are as previously defined, V = D n i (5) in which Vr, D and n? nj are as defined above, where dx of the liquid to be treated, V, Vr, R and dapp are as defined above, where M, V and dapp are as defined above, »/ MX 1 s (9) in which S, V and ht are as defined above, in which ns, ht and hs are as defined above and where the number ns is rounded to the next higher integer. The improved reactor according to claim 5, characterized in that the number of liquid injection n¿nj into the chamber, the volume Vr of liquid contained within the reactor, the volume V of the csorbent bed, the mass M of the absorbent bed, The height ht? the absorbent bed in the reactor and the number ns of the separation members are selected as a function of the volume D of the liquid that will be treated during the period? e treatment t¿, the residence time three which is it requires to obtain the required treatment, the loading time of the reactor tnj, the height hs reached by the liquid by capillary action in the column, the surface S? the reactor and the ratio R of the mass of the saturated absorbent bed with the will be treated to the mass of the same bed in dry form, the dry bed has an apparent density dapp, using the following equations: n inj (1tras + tJ, pJ.) (? 4) ' in which n ^ j, t¿, three and t¿nj, are as defined above, V D r n. . (5) in which Vr, D and n nj are as defined above, vr.dl (R-l) .d app (6) in the gue i of the gueguido that will be treated, V, V2, R and da,? they are as defined above, M = V.dapp (7) in which M, V and dapp are as defined above, ht - (9) in which S, V and ht are as defined above, in which ns, ht and hs are as defined above and where the number ns is rounded to the immediate integer _. higher. 13. The improved reactor according to claim 1, characterized by at least one other input i ':;, > -rr / MX located in the upper portion of the chamber to introduce air into it. 14. The improved reactor according to claim. 3, characterized by at least one other inlet located in the upper portion of the chamber for introducing air into it. 15. The improved reactor according to claim 1. 7, characterized by at least one other inlet located in the upper portion of the chamber for introducing air into it. 16. The improved reactor according to claim :. 8, characterized by at least one other inlet located in the upper portion of the chamber for introducing air into it. 17. The improved reactor according to claim: 9, characterized by at least one other inlet located in the upper portion of the chamber for introducing air into it. 18. The improved reactor according to claim 10, characterized by at least one other inlet located in the upper portion of the chamber for introducing air into it. 19. The improved reactor according to claim. 11, characterized by comprising at least one other entrance located in the upper portion of the chamber for i •• - i / MX introduce air into it. 20. The improved reactor according to claim 12, characterized by at least one other inlet located in the upper portion of the chamber for introducing air therein. - M \