WO1996004065A1

WO1996004065A1 - Adsorption reactor for separating undesirable components from a fluid

Info

Publication number: WO1996004065A1
Application number: PCT/EP1995/002725
Authority: WO
Inventors: Hermann BRÜGGENDICK
Original assignee: Steag Aktiengesellschaft
Priority date: 1994-07-29
Filing date: 1995-07-12
Publication date: 1996-02-15
Also published as: JP3068856B2; JPH10503421A; CA2196217A1; CA2196217C

Abstract

A reactor has a reaction chamber (103) fed with adsorption medium through grid-like feeding funnels and emptied through grid-like discharge funnels (106). The chamber is delimited by multiblade shutters (108, 109) and subdivided into two layers (103a, 103b) by a partition (107). The partition (107) and the downstream shutter (108) substantially have the same structure, i.e. a bar sieve located upstream followed by a stabilising grid to which blades (120 or 110) are connected. The blades are oriented upwards at the partition (107) and downwards at the shutter (108). The reactor may be assembled in a modular manner in the longitudinal and transverse directions from a plurality of reaction chambers.

Description

PCI7EP95 / 02725

1 _Ad sorption reactor for separating undesirable components from a fluid

The invention relates to an adsorption reactor for separating undesired constituents from a fluid, in particular from an exhaust gas, with at least one reaction chamber which has feed means at the top and funnel-shaped extraction means at the bottom for the purpose of or for the removal of a lumpy or granular adsorbent.

DE-OS 26 26 939 shows a device of the generic type, in which the fluid within the reaction space is passed through two layers moving in parallel to one another and the adsorbent is moved in the downstream layer at a higher speed and is loaded less than in the layer the upstream side. With this known device, the exhaust gas should be cleaned as far as possible, since the exhaust gas is still offered sufficient fresh adsorbent on the outflow side. On the other hand, in a relatively thick layer on the outflow side, adsorbent must be continuously drawn off and regenerated, which is only used to a very limited extent. The reaction chamber is divided by vertical partitions. The individual compartments are supplied with adsorbent from a central filling opening and have discharge openings or funnels assigned to the individual layers.

From DE-PS 34 27 905 it is known to even out the adsorbent particle flow through internals over the cross section of the moving bed.

In known adsorption apparatus, essential parts, in particular of the pouring cone in the head region and the discharge cone in the foot region of the reactor, cannot be reached or can only be reached insufficiently by the cross-flowing fluid. The result is hot spots (heat concentrations) up to fire sources in the head area and accumulation of condensate, combined with particle caking in the foot area of the reactor. Difficulties also arise in the area of fluid outflow, since on the one hand the adsorbent is held back and on the other hand the fluid flow is to be prevented as little as possible. The object of the invention is to provide a better flow of the fluid to be treated through the adsorbent bed and to avoid operational disturbances, in particular in the critical head and discharge areas of the adsorber and the fluid outflow.

To achieve this object, the absorption reactor according to the invention is characterized in that the feed means are formed by a grid of several feed funnels arranged side by side and one behind the other and the discharge means are formed by a further grid of discharge funnels arranged side by side and one behind the other; that fluid passages are provided both at least in a downstream blind wall and in the head region of the reaction chamber; and that the downstream blind wall in a sandwich-like construction has a slotted screen on the upstream side with essentially parallel gap limiting elements, then a stabilizing grating with connecting elements running transversely to the gap limiting elements and a downstream louvre construction with slats running transversely to the gap limiting elements.

The material pockets in the head and foot regions of the reactor, which are difficult to reach for the fluid flow, are minimized by dividing the feed and discharge areas of the adsorbent into a large number of conical partial areas. In addition, the particle flow and bulk material mechanics within the reaction space are improved both when the adsorbent is fed in and when it is drawn off by dividing it into partial streams. Although the main flow of the fluid is directed transversely to the adsorbent column, fresh adsorbent in the head region of the reactor is increasingly involved in the reaction due to the fluid introduced there into or out of the reaction space.

The slotted sieve forms a practical, smooth, defect-free surface on which the particle flow of the adsorption can essentially flow from top to bottom in one plane. Particles of normal size are retained on the upstream side by the wall. The fluid flow, on the other hand, is let through virtually the entire height of the blind wall. The crossing arrangement of the gap limiting elements, the stabilizing grid and the slats ensures extremely high dimensional stability, rigidity and stability, so that the properties and the shape of the Venetian blind wall do not change even if the loads on both sides of the Venetian blind Wall fluctuate strongly.

Different pollutants, such as S02 and NOx, and organic substances, such as dioxins and furans and heavy metals, are known to have different reaction speeds with the conventional activated carbon adsorbents. The better adjustability of the adsorption fronts, which is made possible by breaking up the feed and discharge cones, can be used advantageously in a further development of the invention in that various undesirable fluid components, for example mercury, SO2, HC1 and NOx, and organic substances are separated in different vertical adsorption layers and in separate streams ¬ men are removed from the reaction chamber. The flow is divided on at least one vertical partition. The adsorbents drawn off in separate streams can then be subjected to different further processing steps. The adsorbent streams loaded with particularly fast-reacting heavy metals, for example mercury or also organic substances, are disposed of separately. The same applies to adsorbents loaded with SO2 and HCl. In both cases, so-called hearth furnace coke (HOK) is sufficient as adsorbent, that is lignite activated coke, the regeneration of which is uneconomical. In the NOx reduction, however, pelleted hard coal activated coke is preferred as the adsorbent. Its price makes recycling and reuse in a NOx reduction stage economically viable. In an expedient further development of the invention, the fluid is given different flow velocities when flowing through different adsorption layers. Such different flow velocities are particularly useful when different adsorbents, such as HOK and hard coal activated coke, are used in a series connection of several adsorption layers or reaction spaces. The HOK, which is generally obtained as a relatively fine-grained fraction mixture with a particle size between 1 and 4 mm, should be flowed through by the fluid much more slowly than the hard coal activated coke, which is generally uniformly pelleted, for example, with 4 mm. If the same fluid stream is passed in succession through a plurality of adsorption layers, the flow velocities in these adsorption layers can be set by dimensioning the surface area assigned to the adsorption layers.

The invention itself is independent of the type of adsorbent bed used. In addition to the usual moving bed processes, a fixed bed can be used in the invention, which is not continuous, but cyclical, i.e. after extensive loading, is replaced. The use of fixed beds with particularly simple debris material mechanics and operational handling offers itself in the case of the invention due to the possibility of the precise adjustment of the adsorption fronts of different pollutants and the better flow through the entire adsorbent column.

An even more reliable prevention of the formation of condensate in the foot region of the reactor can be achieved in a further development of the invention in that the discharge funnels and / or subsequent discharge pipes are rinsed with the fluid and heated by the fluid. The exiting from a first reaction stage, at least cleaned of some pollutants Fluid is returned under the discharge floor and thereby heats the discharge funnel filled with the adsorbent and their discharge pipes.

However, part of the fluid can also be introduced into the reaction chamber from below through the adsorbent discharge funnel. The effect of the part of the fluid to be cleaned, which is introduced virtually in countercurrent from below, corresponds to that of the partial fluid flow introduced or discharged at the head end; i.e. the amount of adsorbent located in the discharge-side funnels is directly involved in the adsorption, so that even small residues of still unloaded grains can be fully utilized before they are removed.

Since the invention makes it possible to separate different pollutants separately in different vertical adsorptive layers or reaction stages connected in series, the invention is particularly suitable for complex flue gas cleaning in waste incineration plants in which there are typically very different pollutants. The invention makes it possible to separate widely differing components in a fundamentally uniform online process.

A preferred embodiment of the device according to the invention, which combines the advantages of a particularly compact design with optimum adjustability of the inflow surfaces and fluid velocities in the individual adsorption layers, is characterized according to the invention in that at least two ring-shaped reaction chambers are located in a cylindrical housing are arranged concentrically that the two annular chambers for the fluid flow are connected in series and that the inflow area of the first annular chamber for the fluid flow is larger than that of the second annular chamber. A nesting of the at least two annular chambers results in both a compact design and short flow paths. The size of the predominantly cylindrical inflow surfaces can be simply set by appropriate dimensioning of the radii. A uniform flow in the at least two annular chambers can be achieved by radial flow through the annular chambers or the annular adsorbent beds.

An alternative solution to the problem is inventively characterized in that the reaction chamber is arranged in a housing and is delimited by parallel vertical blinds; that the top-side feed means have a feed container for the adsorbent arranged above the reaction chamber and a distribution base formed by a plurality of feed funnels between the feed container and the reaction chamber; that the extraction means have an extraction base formed by a plurality of extraction funnels, which is arranged below the reaction chamber between the latter and a discharge container for the adsorbent; that a fluid inlet in the area of the discharge funnel leads into the housing; that a lower wall is arranged at the level of the discharge base on one side of the reaction chamber between the latter and the housing or a neighboring reaction chamber; that an upper wall is arranged in the region of the distribution floor on the other side of the reaction chamber between the latter and the housing or a neighboring reaction chamber; that the feed container is arranged within the housing, at least one feed pipe for adsorbent leading out of the housing; and that a fluid outlet in the area of the feed container leads out of the housing.

This enables a particularly favorable thermal control of the absorption process. The incoming fluid hits the discharge funnel first. This is essential, as otherwise cooling PCT / EP95 / 02725

tion phenomena, which in extreme cases can lead to caking of the adsorbent. The fluid then acts on the entire side surface of the bed and flows through it, the flow direction being essentially transverse to the bed. Appropriate inlets can also be used to ensure that an upward or angled upward flow is formed in the lower region of the bed. The fluid then rinses the hopper and the entire hopper. The adsorbent is thus already preheated in the feed container so that it is activated as soon as it enters the bed. The surface of the bed below the feed hopper is also subjected to fluid and flows from top to bottom, so that in the case of a fixed bed no dead spaces can form here in which the adsorbent does not take part in the process. Overall, there is an increase in efficiency with optimal use of the adsorbent, malfunctions in the lower region of the bed being avoided.

The heating below the reaction chamber is more intensive the greater the number of discharge hoppers. As a rule, a matrix-like arrangement of the discharge funnels is used. The same conditions exist above the reaction chamber in connection with the feed funnels. The feed pipes, which make it possible to load the feed container from above, are therefore also available for heat transfer.

The device can work with a single reaction chamber. Advantageously, however, the housing contains at least one module consisting of two laterally adjacent reaction chambers. The reaction chambers are therefore parallel to one another, with a common space below the discharge trays and above the feed trays. Each between two adjacent reaction chambers the fluid is guided from bottom to top in order to get into the common upper space containing the feed containers after flowing through the reaction chambers. If several modules are present, this takes place in the spaces between the modules and the housing and in the spaces between adjacent modules. The common space below the discharge floors is fed through a common fluid inlet, which preferably extends over the entire length of the reaction chambers. The same conditions are preferably given for the fluid outlet at the level of the feed container.

In an advantageous further development of the invention, it is proposed that a common feed container and / or a common discharge container is (are) assigned to each module.

A further advantageous embodiment of the invention provides that the upper wall between adjacent reaction chambers is formed by a connecting wall between the adjacent feed containers for the adsorbent or from the common feed container and that a barrier wall leads below the wall from the feed container to the associated blind . The barrier wall is therefore on the inlet side of the reaction chamber and prevents a short-circuit flow in the area of the feed hopper.

In the case of only one reaction chamber, the same advantage is achieved in that the upper wall is arranged between the reaction chamber and the housing below the feed hopper and in that a barrier wall leads from the feed container to the upper wall. The feed funnels arranged one behind the other in the flow direction of the reaction chamber lie with their outlets essentially on a circular arc, the radius of which corresponds to the width of the reaction chamber measured in the flow direction and the center of which lies on the lower edge of the associated barrier wall. In this way, flow conditions are achieved in the head-side area, which roughly correspond to the flow conditions in the rest of the reaction chamber. The adsorbent forms a surface which essentially follows the circular arc. The fluid entering the lower edge of the barrier wall must therefore cover a path regardless of its direction of flow to the surface of the adsorbent, the length of which approximately corresponds to the width of the reaction chamber measured in the direction of flow.

In the case of a moving bed reactor, the adsorbent can be passed through the different layers at different speeds. The layers can also be loaded with different adsorbents.

A particularly advantageous development of the invention is characterized in that a plurality of reaction chambers connect to one another transversely to the flow direction and are provided with common feed containers and / or discharge containers. This allows a modular structure in the longitudinal direction of the reaction chambers. The device can thus be expanded in a modular manner in two mutually perpendicular directions, i.e. Design block-shaped. The fluid inlets and outlets are extended accordingly in the form of a channel. In addition, it is particularly advantageous to arrange between the discharge funnels and the elongated discharge container a discharge device common to the adjoining reaction chambers with at least one discharge rake movable transversely to the flow direction. This extends over the entire length of the discharge container and can be moved back and forth by a single drive.

The reaction chamber is preferably divided by at least one partition into at least two adsorption layers which run essentially vertically and transversely to the direction of the fluid flow, the partition in sandwich-like construction on the inflow side comprising a slotted sieve with essentially parallel gap limiting elements, and then a stabilizing grating with a crosswise direction the gap limiting elements connecting elements and on the outflow side has a Venetian blind construction with slats running transversely to the gap limiting elements.

In a further development of the invention, it is proposed that the slotted screen be provided with slit limiting elements running from top to bottom, the width of the slit being matched to the grain size of the bulk material in such a way that the solid particles except for fine-grained particles in the upstream part be withheld from the reaction chamber.

If the wall construction according to the invention is used on a partition between two reactor layers which run essentially vertically and transversely to the direction of the fluid flow, it may be advantageous to give the partition increased stability since it can be subjected to strongly fluctuating loads, for example by selective Loading or removal of the adsorbent on both sides of the partition. To this end, it is proposed in a further development of the invention that the stabilizing grating on the outflow side has a plurality of strip profiles which cross the connecting elements, the flat sides of the strip profiles running from top to bottom and essentially parallel to the fluid flow direction.

Depending on the arrangement of the Venetian blind construction on an outer boundary wall or a partition located in the reactor itself, the Venetian blind slats preferably have different directions of inclination. In association with a reactor outlet blind, the blind slats primarily have the task of collecting fine-grain particles that have passed through the gap-limiting elements and, if possible, discharging them directly into the discharge container. In this function, the slats, starting from the strip profiles, are inclined upwards, preferably at an angle of approximately 25 to 35 ° to the vertical plane. In contrast, in relation to a partition, the slats of the blind construction have a downward slope. An angle of inclination of 15 to 25 °, in particular approximately 20 ° to the vertical has proven to be advantageous, since at this angle of inclination the advantages of a reliable rejection of the particle flow on the outlet side of the partition and a relatively small wall thickness and compact design are combined.

The use of a slotted screen running over the entire outlet cross-section of the reactor in connection with the stabilizing grid and approximately vertically running belt profiles has two decisive advantages: On the one hand, only fine-grain particles reach the area of the blind construction from the reactor space, so that the tendency to bulge is significantly reduced is; on the other hand, the spaced-apart belt profiles running vertically in the stabilizing grating ensure that the fine-grain particles of the bulk material are easily removed downwards, since they delimit vertical continuous channels or shafts between the slotted screen on the one hand and the louvre construction consisting of inclined slats. The opening cross-section for the fluid remains evenly distributed over the entire height of the outlet blind; this does not change as reactor operation continues. There are practically no longer any bulges which, in all known constructions, have been the cause of more or less strong non-uniformities in the flow resistance and thus in the flow profile of the fluid.

As a partition, the wall component according to the invention creates the prerequisite for the adsorbent flows in the two vertical chambers to have different speeds on both sides of the wall.

The vertical layer on the inlet side to be disposed of as special waste can be largely loaded before it is discharged. The subsequent, at least one further vertical layer in the main body of the adsorbent bed can then are discharged continuously or in batches after a completely different cycle. This layer, which is largely free of highly toxic trace elements, can be disposed of with relatively simple means, reprocessed or correspondingly inexpensively incinerated in normal incineration plants.

The thickness and the cross-section of the individual layers and thus the position of the partition walls can be selected in accordance with certain ingredients or pollutants in the fluid and with regard to a desired separation behavior. In particular, several partition walls can be installed in the reactor such that the cross-flowing fluid flows through at least two partition walls and three layers in succession. Different filling materials (e.g. more or less effective adsorbents) with the same or different filling levels can also be used in the individual layers separated by partition walls. The invention can therefore be used with basically the same advantages regardless of the cross-flow medium used and the adsorbent streams.

The distance from the at least one partition to the fluid outlet blind is preferably several times greater than that to the fluid inlet blind. This has the advantage that the vertical layer on the inlet side has relatively small dimensions and the layer volume can be minimized to the size sufficient for the adsorption of the volatile highly toxic substances.

The wall component according to the invention can be used in an adsorbent reactor both as a delimitation blind on the fluid outlet side of the reactor and as at least one partition with the advantages described.

On the other hand, however, the delimitation blind on the outlet side can also be used in the case of a non-subdivided reactor and, conversely, one or more partition walls of the type according to the invention can be used in conjunction with an otherwise conventional reactor. The invention further relates to a method for cleaning a fluid, in particular a gas, the fluid being passed transversely through at least one vertical bed of granular or lumpy adsorbent and the adsorbent being fed from an overhead feed container onto the bed via feed funnels and below is discharged into a discharge container via discharge funnels. To achieve the object, this method is characterized in that the fluid above the discharge container on one side of the bed of adsorbent is introduced into the area of the discharge funnel, with washing around the discharge funnel below the bed, to the other side thereof, deflected there upwards, passed through the bed and then, after washing around the feed hopper and the feed container, is discharged as a cleaned fluid. This method enables a particularly favorable thermal control of the adsorption process. With optimal use of the adsorbent, the efficiency of the method is increased, while avoiding operational disturbances in the lower area of the adsorbent bed.

After washing around the common area of the discharge funnels of two parallel beds of adsorbent, the fluid is preferably conducted upwards between the beds, passed through the beds on both sides and discharged from a common space which surrounds the feed funnels and the feed containers of both beds .

Advantageous developments of the invention are characterized in the subclaims. Part combinations and subcombinations of the features of the claims are also disclosed as being essential to the invention.

The invention is explained in more detail below with the aid of preferred exemplary embodiments which are shown schematically in the drawing. The drawing shows in: 1 shows a vertical section through an exemplary embodiment of the adsorption reactor according to the invention;

Fig. 2 is a section along the line II-II in Fig. 1;

3 shows a view corresponding to FIG. 1 of a modified embodiment of the invention;

4 shows a vertical section through another exemplary embodiment of the adsorption reactor according to the invention;

Fig. 5 is a section along the line V-V in Fig. 4;

6 shows a perspective view of a further embodiment of a reactor according to the invention;

FIG. 7 shows a detail of the device according to FIG. 6;

Fig. 8 shows a further embodiment of a reactor according to the invention in a representation corresponding to FIG. 6;

FIG. 9 shows a vertical section through part of a reactor corresponding to FIG. 3 with partition and blind walls designed according to the invention;

Fig. 10 is a horizontal section through part of a wall component according to the invention, i.e. a partition or part of the reactor outlet blind according to FIG. 9 with a slatted floor consisting of a slotted sieve, a stabilizing grid and a blind construction (section VII-VII in FIG. 9);

FIG. 11 shows a sectional view, reduced in comparison with FIG. 10, through part of the partition wall;

Fiq. 12 shows a sectional view corresponding to FIG. 11 through part of the reactor outlet blind according to FIG. 9;

FIG. 13 shows a slatted floor arrangement modified compared to the embodiment according to FIG. 12; and ₁ 4 shows a further modified embodiment of a slatted floor arrangement, as can be used both on the outlet blind of the reactor and in the partition. The adsorption reactor 1 shown in FIGS. 1 and 2 in vertical and horizontal sections has a raw gas inlet 2 and a clean gas outlet 3. Between the inlet and outlet, the fluid flows through a first reaction stage 4 and a second reaction stage 5, which are arranged in two reaction chambers connected in parallel 5a and 5b is divided (Fig. 2).

The first reaction stage 4 has a reaction chamber 14 which is rectangular in cross section and which in operation is filled with a bed of bulk material made of particulate or granular adsorbent. On the inlet side, the chamber 14 is delimited by a blind 15 which extends over the full chamber height and on the outlet side by a blind 16 which only extends to a limited height. The adsorbent is fed in from a feed container 7 placed on the chamber 14 via a head-side distribution tray 8. The distribution tray consists in the illustrated embodiment of a uniform grid of side by side and one behind the other in rows and columns arranged square feed funnels 18, in which in connect the feed pipes 19 opening into the chamber 14.

An intermediate floor 8a is installed approximately halfway up the chamber 14. It serves above all to relieve pressure in the case of high adsorption beds and, in the exemplary embodiment shown, has the same design and arrangement (grid of feed hoppers 18a and feed pipes 19a and blocking section 30a) as the distribution floor 8. Also the fluid flow through the cone below of the intermediate floor 8a corresponds to that in the head area. The installation of one or more intermediate trays 8a in the reaction chamber is not necessary, but is often useful. A trigger tray 9 is constructed similarly to the distributor tray 8 from a grid of trigger funnels 20 arranged side by side and one behind the other. Discharge pipes 21 and 22 are connected to the discharge funnels 20. The exhaust pipes 21 are closed by closure elements 23, for example flaps or slides, and the discharge pipes 22 are closed by closure elements 24. To pull the bulk material out of the chamber 14, the closure elements 23, 24 are actuated in a known manner. The exhaust pipes open into different discharge containers 25 and 26, from which the adsorbent loaded with the separated pollutants can be removed for further processing with the aid of suitable conveying devices 27, 28 - shown here as a cellular wheel sluice.

The layer of bulk material corresponding to the inlet-side row of feed hoppers 18 and accordingly also of discharge funnels 20 is preferably separated from the remaining bulk material column by a partition 17 according to the invention (FIG. 3), so that the adsorption layer 40 between the inlet blind 15 and partition 17 is separated by the associated trigger line 20, exhaust pipes 21, discharge container 25 and conveying device 27 can be requested. The same naturally also applies to adsorption layer 41 on the outflow side of partition 17.

The raw gas inlet 2 widens to the overall height dimension of the reaction chamber 14, to the area of the feed funnels 18 and feed tubes 19. The fluid can therefore flow from the side through the blind 15 as well as between the feed tubes 19 from above enter the adsorbent bed through the cones 37 as illustrated by the solid arrows A in FIG. 1. The fluid can therefore reach all bulk bed zones not only with a moving bed, but also with a fixed bed. This means that practically all particles participate in the reaction in the same way.

On the outlet side, there is between the uppermost layer (pouring cone 37) and the upper end of the downstream they 16 provided a blocking section 30 in the form of a closed wall, which prevents a short circuit of the fluid from above directly into the outlet channel 31. The outlet channel 31 merges into a horizontal channel section 32, which runs under the exhaust floor 9. The pre-cleaned fluid leaving the reaction chamber 14 through the outlet channel 31 rinses the discharge funnels 20 and the discharge pipes 21, 22 in the channel section 32 and thereby heats the adsorbent located in these elements to such an extent that the risk of condensation is reliably reduced. The fluid is diverted upward from the channel section 32 into a fluid inlet region 35a and 35b for the two chambers 5a and 5b of the second reaction stage (FIG. 2). The fluid distribution in the two chambers 5a and 5b corresponds in principle to the previously described fluid distribution on the inlet-side blind 15 and the top-side pouring cones 37 of the first reaction stage 4. In the two chambers 5a and 5b, too, feed and discharge funnels are arranged in a grid pattern in order to ensure the most uniform possible Ensure participation of the adsorbent in the entire interior of the chambers 5a and 5b. The removal of the loaded adsorbent usually takes place simultaneously through all of the discharge funnel and tube of the second reaction stage 5a and 5b. The outlet channels 36a and 36b also have a design corresponding to the outlet channel 31 in the region of the outflow-side blind of the two reaction chambers 5a and 5b, so that a large-area cross-flow of the fluid is also ensured in the chambers 5a and 5b. The two channels 36a and 36b unite in the clean gas outlet 3 as shown in FIG. 2.

The two reaction stages 4 and 5 are arranged side by side, the second reaction stage being divided into two subchambers 5a and 5b. This combination combines the advantages of a compact design with good utilization and loading of the adsorbent and simple control options for the adsorption fronts. The channel section 32 may also be made so wide that it extends over the full width of the three reaction chambers 5a, 14 and 5b arranged next to one another and thereby also heats the exhaust pipes of the chambers 5a and 5b.

As can be seen in FIGS. 1 and 3, NH3 is injected as a reducing agent at the deflection point between the outlet channel 31 and the horizontal channel section 32. Of course, other feed points or pre-loading of the hard coal activated coke in the chambers 5a and 5b are also possible.

Also with regard to the shapes and dimensions of the individual funnels 18 and 20, the invention is not subject to any special exceptional conditions. The square or, if appropriate, a rectangular cross-sectional shape shown ensures a particularly large-area utilization of the cross-sectional area for bulk material distribution and a favorable bulk material mechanics. However, other forms are possible with basically the same advantages of the invention.

Often different inflow surfaces of the two reactor stages, in particular larger inflow surfaces of the first stage 4 relative to the second stage 5, are expedient in order to achieve a fluid flow rate that is adapted to the bulk material and adsorption behavior. The first reactor stage can be divided into two parallel subchambers instead of the second reactor stage especially to enlarge their inflow areas. The fluid guidance is then of course reversed from the illustration in FIG. 2.

In the feed containers 7, which are separate for all chambers 5a, 14 and 5b, there is new bulk material for exchanging used adsorbent. It is important that in the adsorption of highly toxic substances and less aggressive media, the loaded adsorbent is separated. In the arrangement described, this takes place simply in that adsorbent layers corresponding to different adsorption fronts into the separate discharge containers 25 and 26 (or in the discharge container of the chambers 5a and 5b) are withdrawn and conveyed from there. These different adsorption layers 40 and 41 are shown in FIG. 3. For example, the largest part of heavy metals, in particular mercury, can be adsorbed in the inlet-side adsorption layer 40 and removed via the exhaust pipes 21 and the discharge container 25.

The embodiment shown in Fig. 3 unterschei¬ det from the embodiment shown in Fig. 1 but also in that the Verteilboden 8 ^■ strδmseite from the inlet side to the exhaust of the reactor 1 'is positioned incrementally. As a result, the blocking section 30 is extended while the adsorption reactor 1 'is otherwise of the same design. 2 also applies to the exemplary embodiment according to FIG. 3.

The raw gas inlet 2 can, however, also extend below the discharge floor 9, in which case 20 suitable openings to the interior of the reaction chamber 14 are formed in the discharge funnels through which raw gas enter, but no granular adsorbent emerges into the fluid inlet distributor can. Such inflow floors are known for example from DE-GM G 87 06 839.8. When the discharge floor 9 is designed as an inflow floor, a barrier section corresponding to the barrier section 30 must also be provided on the rear wall immediately above the floor 9 in order to avoid fluid short circuits to the outlet channel 31.

A blower 38 is arranged with a connecting line between the larger discharge container 26 and the channel section 32 and serves to break up any caking in the individual funnels or in the discharge pipes by means of an artificially forced flow by suction of gas at the start of the adsorbent discharge.

FIGS. 4 and 5 show a preferred embodiment of a two-stage reactor 40 ', the essential components of which are installed in a cylindrical reactor housing 41' are. In the housing 41 'are two annular reaction chambers

₄₄ and ₄ 5 arranged concentrically nested. In the exemplary embodiment described, the chambers ₄ 4 and 45 are filled with different adsorbents, for example the outer chamber 44 with HOK and the inner chamber 45 with pelletized hard coal coke. Accordingly, the outer chamber 44 serves for the separation of the better adsorbable pollutants (corresponding to the first stage 4 of the exemplary embodiment described above) and the inner chamber

45 of the NO _x reduction corresponding to stage 5 of the exemplary embodiment described above. The first and second chambers 44 and 45 are each surrounded by annular fluid outlet channels 46 and 47. A fluid inlet 48 is also designed as an annular channel and is arranged on the radially inner side of the chamber 44. The fluid inlet 49 of the internal second chamber 45 is a central channel which runs along the central axis 50 of the reactor 40 '. The annular fluid inlet 48 of the first reaction chamber 44 and the likewise annular fluid outlet 47 of the second reaction chamber 45 are separated by a partition 51 which is cylindrical in the present case.

A helical inlet channel 52 is arranged in the head region of the reactor housing 41 'coaxially about its central axis 50 and connected to the annular channel serving as the fluid inlet 48 of the first reaction chamber 44. Due to the helical arrangement of the inlet channel 52, the fluid to be cleaned and possibly loaded with solid particles and / or water droplets receives a relatively strong swirl which directs the particles or droplets of higher weight outwards into the area above the pouring cones 37 and between the feed funnels and tubes 18 and 19 of the first reaction stage. The design and arrangement of the feed and discharge funnels and the introduction of the fluid into the two reaction chambers 44 and 45 correspond to those with reference to FIGS. 1 to 3 explained conditions. Due to the circular arrangement and subdivision of the distribution trays 8 and discharge trays 9, the funnels 18 and 20 preferably have a trapezoidal design, as can be seen in FIG. 5.

The design of the blinds or other separating elements for delimiting the reaction chambers 44 and 45 can also correspond to those of the exemplary embodiment described above, although the blinds 55 and 56 (or 65 and 66) on the inflow and outflow sides correspond to the chamber ¬ have an approximately circular design due to sufficient segmentation.

As already mentioned, the uncleaned fluid enters the reactor housing 41 * through the swirling inlet channel 52, reaches the predominantly cylindrical inflow surfaces in the area of the blind 55, crosses the ring-shaped first reaction chamber 44, passes through the outlet side of the reaction chamber outflow-side blind 56 into the outlet channel 46, is directed downward into a circular flow chamber 58 and flows there radially inward in the direction of the central fluid inlet 49 of the second reaction chamber 45. In the circular flow chamber 58, the fluid flows around the discharge funnels 20 and the exhaust pipes 22 similar to the previously described embodiment.

In the central fluid inlet 49, the freed from the more rapidly adsorbed pollutants, ie partially cleaned fluid, is first axially distributed and flows from there according to the arrows in a cross flow or between the feed tubes 19 from above into the bulk material ring of the second reaction chamber 45. Separate the blind 65 the chamber 45 on the inlet side and the blind 66 on the outlet side from the adjacent fluid channels 49 and 47. The fluid outlet channel 47 opens into the head part in a discharge funnel 59, from where the clean gas can be passed into a centrally arranged chimney 60. The inflow area corresponding to the blind 55 of the first reaction chamber 44 is approximately greater in radius than the inflow area corresponding to the blind 65 of the second reaction chamber 45. The flow velocity of the fluid in the first chamber 44 is correspondingly lower in comparison to that in the second Chamber 45. This is also desirable, particularly when using the different adsorbents in the two chambers 44 and 45.

Ring-shaped feed containers 61 and 62 are also arranged above the annular distribution trays 8. A motor-driven distribution device in the form of a rotating rake 63 is arranged in or above the inner feed container 62. The rotating rake 63 levels the bulk material in the container 62 even when it is fed through a single fixed feed nozzle, even if this should be arranged on the side.

The feed container 61 assigned to the first reaction chamber 44 is fed with the aid of a rail wagon 67 through feed openings 68 distributed in a circle around the central axis 50. The lorry runs on a rail rim 69 which is also concentric with the central axis 50. The lore is preferably provided with means for airtight docking to the loading openings 68, an airtight lockable loading space and a blower for pressurizing the loading space. With this design, the excess pressure prevailing in the reaction chamber 44 and thus also in the feed container 61 in the loading space of the wagon 67 can be compensated for, so that no flue gas can escape into the wagon and from there into the ambient atmosphere.

In the embodiment according to FIG. 6, the adsorption reactor has a housing 201 which contains a reaction chamber 202 for adsorbents, in the present case activated coke. The reaction chamber 202 is delimited by blinds 203. Above the reaction chamber 202 there is a feed container 204 from which the reaction medium is passed over a plurality of funnels 205 reaches the reaction chamber. A discharge container 206 is provided below the reaction chamber, which holds the used adsorbent. The latter travels through a plurality of discharge funnels 207.

The gas to be cleaned enters the housing 201 on the left through an inlet 208. A bottom wall 209 prevents the gas from migrating upward directly along the housing. Rather, it is forced to flow around the discharge funnel 207 and heat it up, so that no condensation phenomena can occur there. The gas is then deflected upward to the right by the reaction chamber 202 and flows through the reaction chamber from right to left. The right-hand room is closed off at the top by an upper wall 210. Before the gas can exit through an outlet 211, it is forced to flow around the feed container 204 and the feed funnel 205 in such a way that the top of the feed container is also available for heat transfer. The adsorbent is thus preheated and already enters the reaction chamber 202 in the active state. The feed container 204 is charged with adsorbent via a feed pipe 212. The section of the feed pipe 212 located in the housing 1 is also heated. The reaction chamber 202 contains two schematically indicated partitions 213 and is divided by these into a total of three layers. The layers permit different guidance of the adsorbent or the application of different adsorbent.

As can be seen from FIG. 6, two reaction chambers adjoin one another transversely to the flow direction. This is represented by a schematically indicated partition 214. The feed container 204 and the discharge container 206 are common to both reaction chambers. Furthermore, a continuous discharge rake 215 extends over the entire length of the discharge container 206 and is actuated by a single drive. A barrier wall 216 extends from the feed container 204 to the upper wall 210, the lower edge of which defines the center point of an arc 217 (FIG. 7), the radius of this arc corresponding to the width of the reaction chamber 202 measured in the flow direction. The feed funnels 205 lie with their outlets approximately on this circular arc in order to also approximate the surface of the adsorbent approximately in this circular arc. The gas flowing around the lower edge of the barrier wall 216 thus has to travel essentially the same distance to the surface of the adsorbent as the gas flowing transversely through the reaction chamber 202.

8, the same parts are provided with the same reference numerals.

The modular construction according to the invention in one direction has already been explained with reference to FIG. 6. 8, a total of four elements are placed one behind the other in this direction, see the three indicated intermediate walls 214. Furthermore, FIG. 8 shows that two laterally adjacent reaction chambers 202 are combined to form a module 218 and that the device contains two of these modules . The inlet 208 supplies a common space which is located between the fume cupboards formed by the discharge funnels 207 and the discharge containers 206. The lower walls 209 force the gas into the space between adjacent reaction chambers. The upper walls 210 are formed here by the feed containers 204, each module 218 having a single feed container for its two reaction chambers 202. After flowing through the reaction chambers 202, the gas firstly enters the lateral spaces between the modules 218 and the housing 201 and secondly the central space between the two modules. The two feed containers 204 are in turn in a common space that connects laterally to the channel-shaped outlet 211. Each module has a single discharge container 206. The modular design according to the invention allows any Expansion to maintain the block-shaped construction of the reactor.

In the context of this embodiment, there are certainly possible modifications. Thus, in contrast to FIG. 8, it is possible to work with a single module. It is also possible to use a different type of discharge device instead of the order calculation 215. The channel-shaped inlets and outlets 208 and 211 shown in FIG. 8 can be replaced by individual tubes which lead to a common collector. Furthermore, there is the possibility in FIG. 6 of also arranging the inlet 208 on the end face and the outlet 211 also on the side. Likewise, the ^ inlets and outlets 208 and 211 according to FIG. 8 can be located on the end face.

The dividing walls 213, which are only indicated schematically here, consist of Venetian blind constructions and carry a slotted screen on their upstream side, the slotted bars of which run vertically. Such a slotted screen is also arranged on the upstream side of the outflow-side blind 203.

The partition walls 213 can also be replaced by simple perforated plates.

The partition walls 214 can be partitions or perforated plates. They can also be omitted entirely.

FIG. 9 shows a schematic vertical section through part of an exemplary embodiment of an adsorption reactor 101. In the exemplary embodiment described, the reactor 101 has a rectangular cross section. It has a housing 102 which delimits a reaction chamber 103. Provided in the housing 102 are a distribution base with feed funnels arranged in a matrix for uniform distribution of the bulk material over the cross section of the chamber 103, and a discharge floor 106, 106a with a plurality of discharge funnels for pulling the bulk material out of the chamber 103.

A substantially vertical partition 107 separates the chamber 103 into two adsorption layers 103a and 103b. The layer 103a faces the inlet blind 109 and the layer 103b extends from the outflow side of the partition wall 107 to the opposite reactor outlet blind 108.

The fluid to be treated - in the exemplary embodiment flue gas - flows through the reactor 101 in the manner illustrated by dotted lines or arrows. The flue gas enters the reactor 101 at the bottom, flows around the discharge floor 106 with the discharge funnels and discharge pipes and enters the upstream adsorption layer 103a through a gas inlet box and the inlet blind 109 over most of the overall height of the housing 102. The angle of attack of the slats forming the blinds 109 is 70 ° ± 5 ° to the horizontal in the exemplary embodiment described. The flow in the bed, as the flow lines show, is traversed in the transverse direction. The fluid emerges on the downstream side through the outlet blind 108 and its slats 110 into a gas outlet box. The outlet-side wall construction has the slats 110 arranged vertically one above the other, which in the exemplary embodiment described are set at an angle of 60 ° ± 5 °, preferably 60 ° to 65 °, to the horizontal.

The new aspects according to the invention relate above all to the design of the partition wall 107 running vertically in the exemplary embodiment described and the very similarly designed blind 108 of the reactor housing 102. These new aspects are described below with reference to the schematic partial views according to FIG. 10 to 12 are explained in more detail.

As shown above all in the enlarged horizontal sectional view according to FIG. 10, the partition wall 107 or the blind 108 is designed as a slatted floor. The latter consists of an upstream slotted screen 113 with rod-shaped slit limiting elements 113a which run from top to bottom and have a uniform triangular cross section. The slotted screen 113 is connected to a stabilizing grid 114 in a sandwich-like manner. at With the usual grain size of the activated coke used as the adsorbent, the gap limiting elements 113a have a gap width of 1.25 mm ± 0.5 mm, a profile side length of 2.2 mm ± 0.5 mm facing the activated coke bed and a depth to the stabilizing grid of 4.5 mm ± 1mm. However, these dimensions correspond only to an exemplary embodiment realized in a prototype; in particular, the width of the gap 113b between two adjacent gap limiting elements 113a suitably depends on the size of the bulk material particles which are to be retained by the gap screen in the inlet-side adsorption layer 103a (or in the case of the blind 108 in the outlet-side adsorption layer 103b).

According to FIG. 10, the stabilizing grating 114 consists of connecting rods 115, which run transversely to the gap-limiting elements 113a, and of strip profiles 116 arranged at a greater distance parallel to the gap-limiting elements. The longitudinal rod-shaped gap-limiting elements 113a. are spot-welded to the connecting rods 115, which are arranged one above the other; on the other hand, the band profiles 116 are welded to the transverse connecting rods 115. Optionally, the narrow sides facing away from the connecting rods 115 can be connected, in particular welded, with rotated square rods 118 in the manner shown in FIG. 10. These square bars are commercially available as a unit with the band profiles 116 (for other purposes) and are therefore also used here. The square bars 118 can also be provided instead of the rectangular or round connecting bars 115.

As stated above, the outlet blind 108 of the reaction chamber 103 in the exemplary embodiment described is provided with the same, approximately vertically running gap floor 112 as the partition 107. In this respect, the bulk material is retained on the upstream side at least to the extent that both the partition wall 107 and the blind 108 on the gap floors 112 its particle diameter is larger than the gap width 113b of the slotted sieve 113. As far as small grain particles can penetrate the gaps 113b in the direction of fluid flow (arrow A in FIG. 10), they reach vertical channels 117 formed between the flat sides of the profiles 116 and fall through them (Continuous) channels down to a discharge area, which is designated with 119 for the outlet blind in FIG. In the discharge area, these fine-grain particles are either fed back to the adjacent discharge funnel of the discharge floor 106 or, if appropriate, also discharged separately in order to continuously reduce the technologically unfavorable dust constituents.

In contrast to conventional cross-flow adsorbers, no noticeable bulk material bulges form on the inclined lamellae 110 on the outlet side of the housing 102, so that the fluid encounters a uniform flow resistance on the outflow side over the entire height of the housing. In this respect, the angle of inclination of the individual slats 110 of the blind is also not critical; however, the angle of inclination is preferably sufficiently large to allow bulk material impinging on the lamella 110 to flow back into the channels 117 or to let them flow away. For this purpose, an angle of approximately 60 ° ± 5 ° to the horizontal plane for the slats 110 has proven to be expedient.

If the slats of the partition wall 107 and the louver 108 have the same configuration, the partition wall 107 has a different arrangement of the louver slats 120 on the outflow side facing the adsorption layer 103b. The slats 120 are inclined downwards from the slit bottom 112 and in the direction of the layer 103b arranged. An angle of inclination to the vertical of 20 ° ± 5 ° has proven to be favorable, on the one hand to ensure a relatively free passage of fluid and on the other hand to reliably prevent bulk material from passing from layer 103b into layer 103a on the entry side. At the acute angle to the vertical there is also Space requirement of the wall 107 including the fins 120 in the reactor is still acceptably small.

As can be seen, the bulk material columns in the layers 103a and 103b separated from one another by the wall 107 are separated continuously from one another into the discharge area assigned to them in each case. In particular, the inlet-side layer 103a has its own discharge funnel 106a. The larger particles emerging from the layer 103a through the gap-limiting elements 113a fall vertically downwards through the channels 117 when they enter the space between the band profiles 116 and are discharged from the wall 119 'into the discharge funnel 106a. A passage of these loaded particles into the layer 103b is prevented. The adsorbent column located in the relatively narrow layer 103a can be emptied via the discharge funnel 106a independently of the main bed of the layer 103b and can be disposed of appropriately, for example as special waste, in a combustion plant. Experience has shown that almost all highly toxic components, such as dioxins and furans, are separated by adsorption in this relatively thin layer. After passing through the partition wall 107, the other pollutants are adsorptively deposited in a subsequent layer 103b along a path length of the fluid that is 9 times longer, for example. Disposing of the used or loaded adsorbent from layer 103b is comparatively simple and easy. This adsorbent can optionally also be regenerated and returned to the reactor 101.

A continuous formation of both the gap limiting elements 113a and the strip profiles 116 running parallel to them (with a considerably greater distance) is generally preferred for reasons of cost. On the other hand, these vertically extending components 113a and 116 can, however, also be assembled from several parts either in abutment or with toothing or overlap. Especially for the Belt profiles 116 are sufficient if they extend over a partial length of the reactor height in such a way that the fins 110 of the blind can be fastened, in particular welded, to them. An interruption of the belt profiles 116 is of no importance for the reliable removal of the small grain particles through the channels 117, since an exchange of particles between adjacent channels 117 does not impair the particle guidance from top to bottom and the inclined lamellae 110 also have a directional effect obliquely downwards.

13 and 14 show embodiments of slatted floors 140 and 150, in which the slotted screen each consists of a plurality of vertical sections 141a, 141b and 151a ... 151c, which are arranged to overlap. In the embodiment according to FIG. 13, each slotted wire section is cranked twice at its upper end 142 and engages behind the lower end of the higher slotted wire section 141a. The individual gap limiting rods are aligned vertically with one another in the overlapping gap screen sections 141a and 141b. Also in the modified embodiment according to FIG. 13, a stabilizing grating 144 with transverse connecting rods 145 and band profiles 146 delimiting extraction channels 117 is provided. The belt profiles 146 are, however, interrupted vertically and assigned only to the flat parts of the slotted wire sections 141a and 141b. The blind slats connected to the band profiles 146 are not shown in FIGS. 13 and 14.

In the embodiment in FIG. 13, the vertical delimitation plane of the bulk material bed is interrupted in the overlap region of the slotted screen sections 141a and 141b. A small bulge 147 forms there. Because of the free space in the area of the overlap point beyond the bulge 147, the increase in the flow resistance is not significant there. The interruption of the gap delimiting elements or the gap 113b formed between them has the advantage, however, that bulk material parcels trapped, particularly elongated, in columns 113b Part by section, namely in the area of the bulge 147, can come out of the gap guide and can reorient.

A similar effect is achieved in the modified embodiment shown in FIG. 14. The effective gap limiting elements in the gap screen sections 151a to 151c predominantly run somewhat inclined to the generally vertical direction of travel of the bulk material in the reactor chamber 103. Because of the inclined inclination of the gap screen sections, only one offset in the overlap area 152 is provided in the embodiment according to FIG. 14 .

In the embodiment according to FIG. 14, a stabilizing grid is individually assigned to the slotted screen sections 151a ... 151c. 14 shows only the transverse connecting rods 155.

Numerous modifications are possible within the scope of the inventive concept. Thus, the individual components belonging to the slatted floor 112 can have predominantly rounded edges and, taking into account the stabilization requirements, can have large distances and / or small wall thicknesses. The outflow side can, if appropriate, also be horizontally curved or polygonal and sectionally flat. The design of the Jalou¬ is not critical because of the special support and holding function of the slit bottom 112, 140 and 150. The size of the channels should, if possible, be selected so that on the one hand the space requirement is small and on the other hand a reliable removal of the bulk material particles penetrating the slotted screen is ensured under the influence of gravity.

Furthermore, within the scope of the invention it is readily possible to work with a single adsorption layer. The flow direction of the fluid can also be reversed in FIG. 1, for example, so that the raw gas enters the adsorber 1 at 3 and leaves the latter at 2. The raw gas then emerges from the head of the adsorption layer.

Claims

Pat-.ent.anfiprύche

1. adsorption reactor for separating undesired constituents from a fluid, in particular from an exhaust gas, with at least one reaction chamber (14; 103) which has feed means at the top and funnel-shaped take-off means at the bottom for charging or removing a lumpy or granular adsorbent β, characterized in that the feed means are formed by a grid of a plurality of feed funnels (18) arranged next to and behind one another and the discharge means by a further grid of discharge funnels (20; 106) arranged next to and behind one another; that fluid passages are provided at least in a louver wall (16; 108) on the downstream side and in the head region of the reaction chamber; and that the downstream Jalou¬ sie wall (16; 108) in sandwich-like construction on the inflow side a slotted screen (113; 141; 151) with essentially parallel gap limiting elements (131a), then a stabilizing grille (114; 144) with transverse to the connecting elements (115; 145; 155) extending the gap limiting elements and a venetian blind construction on the outflow side with slats (110) running transverse to the gap limiting elements.

2. Adsorption reactor according to claim 1, characterized gekennzeich¬ net that at least two separate reaction chambers (4, 5a, 5b; 40, 41), which can be filled and emptied independently of each other with adsorbent, are arranged spatially side by side and are connected in series for the fluid flow.

3. Adsorption reactor according to claim 1 or 2, characterized in that the discharge funnel (20) and / or there subsequent exhaust pipes (21, 22) are arranged in the flow path (32) of the fluid to be cleaned.

4. Adsorption reactor according to one of claims 1 to 3, da¬ characterized in that an exhaust gas duct (32) downstream of the exhaust gas outlet (31) of a reactor stage (4) and below the (4) bottom (9) is arranged such that the discharge funnel (20) and tube (21, 22) are flushed by the fluid with heating.

5. Adsorption reactor according to one of claims 1 to 4, da¬ characterized in that the bottom-side funnel grid (20) is provided with openings for the passage of the fluid to be cleaned and that the openings are connected to the fluid inlet (2).

6. Adsorption reactor according to one of claims 1 to 5, da¬ characterized in that the fluid inlet (2) extends approximately over the entire height of the reaction chamber, while the fluid outlet (31) only a limited height of the outlet side of the reactor (1) spanned in order to avoid flow short-circuits in the head region of the reaction chamber.

7. Adsorption reactor according to claim 4, characterized gekennzeich¬ net that a first reactor stage (4) is flanked on both sides by second reactor stages (5a, 5b) and that the fluid stream returned under the bottom (9) of the first reactor stage is divided into at least two parallel substreams and into the two reactor stages (5a, 5b) flanking the first reactor stage (4).

8. Adsorption reactor according to one of claims 1 to 7, da¬ characterized in that several rows (18 ') of hopper funnel (18) from the fluid inlet (2) are arranged one behind the other at stepped heights.

9. Adsorption reactor for separating undesired constituents from a fluid, in particular from an exhaust gas, with at least one reaction space (44, 45), the top-side feed means and bottom-side funnel-shaped extraction means for feeding in or for removing a lumpy or granular adsorbent , in particular according to one of claims 1 to 8, characterized in that at least two annular reaction chambers (44, 45) are arranged concentrically in a cylindrical housing (41), that the two annular chambers (44, 45) are connected in series for the fluid flow and that the flow areas of the first annular chamber (44) for the fluid flow are larger than that of the second annular chamber (45).

10. Adsorption reactor according to claim 9, characterized gekenn¬ characterized in that the inflow and outflow pools of the two annular chambers (44, 45) are arranged so that the annular chamber is flowed through substantially radially, preferably from the inside to the outside of fluid.

11. Adsorption reactor according to claim 10, characterized gekenn¬ characterized in that the first and second annular chambers (44, 45) are surrounded by annular fluid outlet channels (46, 47), that the fluid inlet for the first annular chamber (44) also as an annular channel ( 48) and that the fluid inlet (48) of the first ring chamber and the fluid outlet (47) of the second ring chamber (45) are separated by a cylindrical partition (51).

12. Adsorption reactor according to one of claims 9 to 11, characterized in that a circular flow chamber (58), which connects the fluid outlet (46) of the first annular chamber (44) to the fluid inlet (49) of the second annular chamber (45), is arranged under the fume cupboards (9) in such a way that the exhaust funnel (20) and / or exhaust pipes (22) are washed and heated by the partially cleaned fluid flowing radially from the outside inwards.

13. Adsorption reactor according to one of claims 9 to 12, characterized in that a helical inlet channel (52) is arranged in the head region of the reactor housing (41 ') about its central axis (50) and with the fluid inlet (47) of the first annular chamber (44 ) connected is.

14. Adsorption reactor according to one of claims 9 to 13, characterized in that the distribution (8) and Abzugsbδden (9) ring-shaped and the funnel (18, 20) are designed trapezoidal ge.

15. Adsorption reactor according to one of claims 9 to 14, characterized in that annular feed containers (61, 62) are arranged above the annular distribution trays (8).

16. Adsorption reactor according to claim 15, characterized gekenn¬ characterized in that a motor-driven circumferential distribution device (63) is mounted on a with the vertical housing axis (50) coincident rotary axis in an annular feed container (62).

17. Adsorption reactor according to claim 15 or 16, characterized in that in a top wall of an annular feed container (61) uniform charging openings (68) are arranged at an equal distance around the housing axis (50) and that a rail ring (69) in a corresponding manner radial distance above the top wall is arranged.

18. Adsorption reactor according to claim 17, characterized gekenn¬ characterized in that on the rail ring (69) running rail vehicle (67) with means for preferably airtight docking to the loading openings (68), an airtight lockable loading space and a blower for pressurization the cargo hold is provided.

19. Adsorption reactor for separating undesired constituents from a fluid, in particular from an exhaust gas, with at least one reaction chamber (202) which has feed means at the top and funnel-shaped take-off means at the top for feeding or removing a lumpy or granular adsorbent, in particular after one of claims 1 to 18, characterized in that the reaction chamber (202) is arranged in a housing (201) and is delimited by parallel vertical blinds (203); that the top-side feed means have a feed container (204) for the adsorbent arranged above the reaction chamber (202) and a distribution base formed by a plurality of feed funnels (205) between the feed container (204) and the reaction chamber (202) iron; that the extraction means have an extraction base formed by a plurality of extraction funnels (207), which is arranged below the reaction chamber (202) between the latter and a discharge container (206) for the adsorbent; that a fluid inlet (208) leads into the housing (201) in the region of the discharge funnel (207); that a lower wall (209) is arranged at the level of the discharge base on one side of the reaction chamber (202) between the latter and the housing (201) or an adjacent reaction chamber (202); that an upper wall (210) is arranged in the region of the distribution floor to the other side of the reaction chamber (202) between the latter and the housing (201) or an adjacent reaction chamber (202); that the feed container (204) is arranged inside the housing (201), at least one feed pipe (212) for adsorbent leading out of the housing (201); and that a fluid outlet (211) leads out of the housing (201) in the region of the feed container (204).

20. The apparatus according to claim 19, characterized in that the housing (201) contains at least one module (218) consisting of two laterally adjacent reaction chambers (202).

21. The apparatus according to claim 20, characterized in that each module (218) is (are) associated with a common feed container (204) and / or a common discharge container (206).

22. The apparatus of claim 20 or 21, characterized gekenn¬ characterized in that the upper wall (210) between adjacent reaction chambers (202) from a connecting wall between the adjacent feed containers (204) for the adsorbent or from the common feed container (204 ) is formed and that below the wall (210) each a barrier wall (216) leads from the feed container (204) to the associated blind (203).

23. The apparatus according to claim 19, characterized in that the upper wall (210) between the reaction chamber (202) and the housing (201) below the feed hopper (205) is angeord¬ net and that a barrier wall (216) from the feed container (204 ) leads to the upper wall (210).

24. Device according to one of claims 19 to 23, characterized in that the feed funnel (205) arranged one behind the other in the flow direction of the reaction chamber (202) lie with their outlets essentially on a circular arc, the radius of which is the width of the reaction chamber measured in the flow direction (202) corresponds and whose center lies on the lower edge of the associated barrier wall (216).

25. Device according to one of claims 19 to 24, characterized in that a plurality of reaction chambers (202) connect to each other transversely to the flow direction and with common feed containers (204) and / or discharge containers

(206) are provided.

26. The apparatus according to claim 25, characterized in that between the discharge funnels (207) and the elongated discharge container (206) is arranged a discharge device common to the adjoining reaction chambers (202) with at least one discharge rake (215) movable transversely to the flow direction .

27. Adsorption reactor according to one of claims 1 to 26, characterized in that the reaction chamber (14; 103; 202) by at least one partition (17; 107; 213) in at least two adsorption layers which run essentially vertically and transversely to the fluid flow direction (40, 41; 103a, 103b) and that each layer has several feed and discharge funnels (18; 20; 207) with separately operable closure and / or metering devices (23, 27 and 24, 28).

28. Adsorption reactor according to claim 27, characterized gekenn¬ characterized in that the partition (17; 107; 213) in sandwich-like construction on the upstream side of a slotted screen (113; 141; 151) with essentially parallel gap limiting elements (113a), then a stabilizing grid (114; 144) with connecting elements running transversely to the gap limiting elements

(115; 145; 155) and on the outflow side a blind construction with slats running transversely to the gap limiting elements

(120).

29. Adsorption reactor according to one of claims 1 to 28, characterized in that the stabilizing grid (114; 144) has a plurality of belt profiles (116; 146) which cross the connecting elements (115; 145; 155).

30. Adsorption reactor according to one of claims 1 to 29, characterized in that the slotted screen (113; 141; 151) with gap limiting elements running from top to bottom

(113a) is provided, the width of the gap (113b) being matched to the grain size of the bulk material so that the solid particles are retained except for fine-grain particles in the upstream part of the reactor (103, 103a).

31. Adsorption reactor according to one of claims 1 to 30, characterized in that the flat sides of the band elements (115; 145; 155) crossing band profiles (116; 146) run from top to bottom and essentially parallel to the fluid flow direction (A) .

32. Adsorption reactor according to one of claims 1 to 31, characterized in that the gap-limiting elements (113a) have approximately triangular cross-sectional profiles, one side of which the fluid flows against and the opposite side of the upstream side with the transverse connecting elements (115; 145; 155 ) of the stabilizing grid (114, 144) is connected.

33. Adsorption reactor according to claim 31 or 32, characterized in that between two adjacent Band¬ profiles (116) of the stabilizing grating (114) is provided a substantially vertical channel (117) for removing small grain particles passing through the slotted screen.

34. Adsorption reactor according to claim 33, characterized gekenn¬ characterized in that between the belt profiles (116) formed channels (117) open at the lower end in a discharge funnel.

35. Adsorption reactor according to one of claims 1 to 34, characterized in that the gap limiting elements (113a) are designed as straight rods.

36. Adsorption reactor according to one of claims 1 to 35, characterized in that the slotted screen consists of several verti¬ cal sections (141a, 141b; 151a ... 151c), which are arranged such that they overlap such that the higher-lying slit section (141a , 151a) overlaps the lower section (141b; 151b) to the reaction chamber (103).

37. Adsorption reactor according to claim 36, characterized gekenn¬ characterized in that the upper end (142; 152) of each gap section (141a, 141b; 151a ... 151c) is cranked.

38. Adsorption reactor according to claim 36 or 37, characterized in that the individual gap limiting elements

(113) of each slotted wire section (141a; 151a) are aligned with those of the adjacent slotted wire sections (141b; 151b).

39. Adsorption reactor according to claim 37 or 38, characterized in that each slotted screen section (141a, 141b) own stabilizing grid (144) is assigned, which is connected to a flat area of the slotted wire section.

40. Adsorption reactor according to one of claims 1 to 27 and 29 to 39, characterized in that the lamellae (110) of the blind construction are arranged inclined upwards.

41. Adsorption reactor according to claim 40, characterized gekenn¬ characterized in that the blind slats (110) are arranged inclined at an angle between 25 and 35 ° to the vertical.

42. Adsorption reactor according to one of claims 33 to 41, characterized in that the fins (110) of the Jalousiekon¬ construction to the vertical channels (117) arranged so inclined that the bulk material on the fins under the influence of gravity in the channels is directed.

43. Adsorption reactor according to one of claims 28 to 39, characterized in that the fins (120) of the Jalousiekon¬ construction are inclined obliquely downwards.

44. adsorption reactor according to claim 43, characterized gekenn¬ characterized in that the blind slats (120) are arranged inclined at an angle between 15 and 25 ° to the vertical.

45. Adsorption reactor according to one of claims 27 to 44, characterized in that the distance of the at least one partition (107) to the fluid outlet blind (108) is several times larger than that to the fluid inlet blind (109).

46. A method for cleaning a fluid, in particular a gas, the fluid being passed across at least one vertical bed of granular or particulate adsorbent is and wherein the adsorbent is fed from an overhead feed container via the feed hopper onto the bed and is discharged below the discharge hopper into a discharge container, characterized in that the fluid above the discharge container on one side of the bed of adsorbent is introduced into the area of the discharge hopper , with washing around the discharge funnel below the bed to the other side thereof, deflected there upwards, passed through the bed and then, after washing around, the feed hopper and the feed container are discharged as cleaned fluid.

47. The method according to claim 46, characterized in that after washing around the common area of the discharge funnel of two parallel beds of adsorbent between the beds, the fluid is guided upward, passed through the beds on both sides and discharged from a common space which surrounds the hopper and hopper of both beds.