EP0449833A1

EP0449833A1 - Process and device for separating undesirable constituents from waste gases

Info

Publication number: EP0449833A1
Application number: EP89907728A
Authority: EP
Inventors: Hermann BRÜGGENDICK
Original assignee: Steag GmbH
Current assignee: Steag GmbH
Priority date: 1988-12-30
Filing date: 1989-07-13
Publication date: 1991-10-09
Also published as: FI913136A0; DD283945A5; US5344631A; WO1990007371A1; CZ443389A3; CZ283690B6; DK127891D0; DK170549B1; PL160703B1; EP0376356A1; DK127891A; SK443389A3; US5344616A; FI92373B; YU171189A; ATE90223T1; SK279613B6; DE3844422A1; FI92373C; DE58904635D1

Abstract

L'adsorbant en morceaux ou en granules est introduit dans l'encei nte réactionnelle (14) puis évacué de cette dernière à travers plusieurs entonnoirs distincts de chargement et d'évacuation (18 et 20) répartis en réseaux. Le gaz brut est introduit, pour la majeure partie, sur tout le côté d'admission, perpendiculairement à l'enceinte réactionnelle et, en moindre quantité, par le haut, à travers le cône de distribution de produits en vrac (17), dans l'enceinte réactionnelle, et traverse cette dernière (14) avec une répartition telle que le milieu réactionnel participe uniformément à l'adsorption, pratiquement dans la totalité des zones de l'enceinte réactionnelle. Plusieurs chambres de réaction à couches réactionnelles multiples sont disposées en série dans le parcours du fluide. Après avoir quitté le premier stade de la réaction (14), le fluide partiellement épuré est recyclé sous le fond de décharge (9), de manière à s'écouler autour des entonnoirs d'évacuation (20) et de leurs tuyaux de décharge (21, 22) et à les chauffer, ce qui empêche la formation d'un condensat. L'adsorbant (1) peut être utilisé pour l'épuration des gaz de fumée, dans les usines d'incinération d'ordures ménagères, opération au cours de laquelle différents constituants fluides indésirables peuvent être retirés séparément dans diverses couches d'adsorption (25, 27 ou 26, 28) et soumis à un traitement ultérieur.The adsorbent in pieces or in granules is introduced into the reaction vessel (14) then evacuated from the latter through several separate loading and evacuation funnels (18 and 20) distributed in networks. The raw gas is introduced, for the most part, over the entire intake side, perpendicular to the reaction chamber and, in a smaller quantity, from above, through the cone for distributing bulk products (17), into the reaction vessel, and crosses the latter (14) with a distribution such that the reaction medium participates uniformly in the adsorption, practically in all of the zones of the reaction vessel. Several reaction chambers with multiple reaction layers are arranged in series in the path of the fluid. After leaving the first stage of the reaction (14), the partially purified fluid is recycled under the discharge bottom (9), so as to flow around the discharge funnels (20) and their discharge pipes ( 21, 22) and to heat them, which prevents the formation of condensate. The adsorbent (1) can be used for the purification of flue gases in household waste incineration plants, an operation during which different undesirable fluid constituents can be removed separately in various adsorption layers (25 , 27 or 26, 28) and subject to further processing.

Description

Method and device for separating undesired components from an exhaust gas

The invention relates to a method for separating undesirable components from a fluid, in particular an _A bgas, sorbents by adsorption on a lumpy or granular Ad¬, wherein the exhaust gas flows to be treated at least one adsorbent-filled reaction chamber and through at least one adsorption layer durch¬ is directed. The invention further relates to a device for performing this method.

DE-OS 26 26 939 shows a method of the generic type

Type in which the fluid is passed within the reaction space through two layers moving parallel to one another and the adsorbent is moved at a higher speed in the downstream layer and is loaded less than in the layer on the upstream side. This known method is intended to purify the exhaust gas as far as possible, since enough fresh adsorbent is still offered to the exhaust gas 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 equalize the adsorbent particle flow by means of 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. The invention is based on the object of ensuring a better flow of the fluid to be treated through the adsorbent bed and of avoiding operational disturbances, in particular in the critical head and exhaust areas of the adsorber.

Starting from a method of the type mentioned at the outset, the invention provides for this object that the adsorbent is introduced into and separated from the reaction space in a grid-like manner through a plurality of separate feed and discharge funnels, and that the fluid is partly from the side is guided transversely to the adsorption layer and partially vertically through the reaction space in such a way that the adsorbent takes part in the adsorption practically uniformly in all zones of the reaction space. It is particularly advantageous that the exhaust gas is passed through at least two separate adsorption layers and that the fluid is partially introduced into the reaction chamber from above.

In terms of device, there is the solution to the above. The object of the invention is that the feed means are formed by a grid of several feed funnels arranged side by side and one behind the other and the trigger means are formed by a further grid of feed funnels arranged side by side and one behind the other and that both at least on one side and in the head Rich of the reaction chamber fluid passages are provided.

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 mechanics within the Reaction space improved both when giving up and when removing the adsorbent by dividing 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.

Different pollutants, such as S0 ₂ and NO, are known to have different reaction speeds with the usual activated carbon adsorbents. The better adjustability of the adsorption fronts, which is made possible by breaking up the feed and discharge cones, can advantageously be used in a further development of the invention in that various undesirable fluid components, for example mercury, SO, HC1 and NO, are separated in different vertical adsorption layers and separated in separate streams be discharged into the reaction room. 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, are disposed of separately. The same applies to adsorbents loaded with S0 ₂ and HC1. In both cases, so-called hearth furnace coke (HOK) is sufficient as the adsorbent, that is lignite activated coke, the regeneration of which is uneconomical. In contrast, in the case of NO reduction, pelletized hard coal activated coke is preferred as the adsorbent. Its price makes reprocessing and reuse in an NO _χ reduction stage economically sensible.

In an expedient further development of the method, 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 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 flow through 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 inflow surfaces assigned to the adsorption layers.

The invention itself is independent of the type of bed of adsorbent used. In contrast to the usual moving bed processes, the invention preferably uses a fixed bed which is not continuous, but cyclical, i.e. after extensive loading, is replaced. The use of fixed beds with particularly simple bulk material mechanics and operational handling offers itself in the invention due to the possibility of the precise setting 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 fluid emerging from a first reaction stage and at least cleaned of some pollutants is returned under the distribution floor and warmed thereby the discharge funnel filled with the adsorbent and their discharge pipes.

However, part of the fluid can also be introduced into the reaction space from below through the adsorbent discharge funnel. The effect of the part of the fluid to be cleaned, which is virtually introduced in countercurrent from below, corresponds to that of the partial flow of fluid introduced or discharged at the head; 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 process according to the invention enables separate separation of different pollutants in different vertical adsorbent layers or reaction stages connected in series, the process according to 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 constituents in a fundamentally uniform online process.

A preferred embodiment of the device according to the invention, which combines the advantages of a particularly compact construction 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 spaces in a cylindrical housing are arranged concentrically that the two annular spaces for the fluid flow are connected in series and that the flow area of the first annular space for the fluid flow is larger than that of the second annular space. If the at least two ring spaces are nested, both result in a compact design as well as short flow paths. The size of the predominantly cylindrical inflow surfaces can easily be adjusted by suitable dimensioning of the radii. A uniform flow in the at least two annular spaces can be achieved by radial flow through the annular spaces or the annular adsorbent beds.

Appropriate developments of the device according to the invention are characterized in the subordinate claims. Partial combinations and subcombinations of the features of the claims are also disclosed as being essential to the invention.

In the following, the invention is explained in more detail with reference to exemplary embodiments schematically shown in the drawing. The drawing shows:

Fig. 1 is a vertical section through an exemplified embodiment of the invention Adsorptionsvorrich- ^'processing;

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

FIG. 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 device according to the invention; and

FIG. 5 is a sectional view along the section line V-V in FIG. 4.

The vertical and horizontal sections in FIGS. The illustrated adsorber 1 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, which is divided into two parallel reaction chambers 5a and 5b (FIG. 2).

The first reaction stage 4 has a reaction chamber 14 with a rectangular cross section, which in operation is filled with a bulk bed of lumpy 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 storage container 7 placed on the chamber 14 via a distribution plate 8 on the top side. The distribution plate consists of a uniform grid in the illustrated embodiment of a square feed hopper 18 arranged next to one another and one behind the other in rows and columns. connect to the feed pipes 19 opening into the chamber 14.

An intermediate floor 8a is installed approximately halfway up the chamber 14. It serves primarily to relieve pressure in the case of high adsorption beds and, in the exemplary embodiment shown, has the same design and arrangement (grid of feeder funnels 18a and feeder tubes 19a and blocking section 30a) as the distribution floor 8. Also, the fluid flow through the cone of material below the intermediate floor 8a corresponds to that in the head area. The installation of one or more intermediate shelves 8a in the reaction chamber is not necessary, but is often expedient.

A discharge floor 9 is constructed similarly to the distribution floor 8 from a grid of discharge funnels 20 arranged side by side and one behind the other. Close the discharge funnel 20 exhaust pipes 21 or 22. The exhaust pipes 21 are closed by closure elements, for example flaps or slides 23, and the exhaust pipes 22 are closed by closure elements 24. To remove the bulk material from the chamber 14, the closure elements 23, 24 are actuated in a known manner. The discharge pipes open into different collecting 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 means - shown here as cellular wheel sluice 27, 28.

The bulk material layer corresponding to the inlet-side row 18 'of feed hoppers and, accordingly, also of discharge funnels 20 is preferably separated from the remaining bulk material column by a suitable shutter 17 or other suitable guide elements (FIG. 3), so that the adsorption layer 40 is between them Inlet a ^' lousie 15 and partition 17 can be removed separately via the associated discharge funnel 20, discharge pipes 21, collecting container 25 and conveyor 27. The same naturally also applies to bulk material layers 41 on the outflow side of the partition 17.

The raw gas inlet 2 expands 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 pass through the blind 15 from the side as well as between the feed tubes 19 from above the cones of bulk 37 enter the adsorbent bed, as illustrated by the solid arrows A in Fig. 1. The fluid can therefore reach all bulk material bed zones not only in the case of a moving bed, but also in the case of a fixed bed. This means that practically all particles participate in the reaction in the same way.

On the outlet side is between the top layer (bulk cone 37) and the upper end of the outflow-side blind 16, a blocking section in the form of a closed wall 30 is provided, 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 through the discharge passage 31, the ^'reaction chamber 14 leaving vorgereinig¬ te fluid flows around the discharge hoppers 20 and the discharge tubes 21, 22 in the channel portion 32 and heated thereby, the adsorbent located in these elements so far, is that a Kon¬ densation reliably prevented. 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. The feed and discharge funnels are also arranged in a grid pattern in the two chambers 5a and 5b, in order to ensure the most uniform possible 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 area of the outflow-side blinds of the two reaction chambers 5a and 5b, so that a large-area transverse flow of the fluid is also ensured in the chambers 5a and 5b. The two channels 36a and 36b unite as shown in FIG. 2 in the clean gas outlet 3.

The two reaction stages 4 and 5 are arranged side by side, the second reaction stage in two subchambers 5a and 5b is divided. This combination combines the advantages of a compact design with good utilization and loading of the adsorbents and simple control options for the adsorption fronts.

The channel section 32 may possibly can also be made so wide that it extends over the full surface of the three reaction chambers 5a, 4 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, the reducing agent NH is injected 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 coke in the chambers 5a and 5b are also possible.

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 that the cross-sectional area on the bulk material distribution is used in a particularly large area and that the bulk material mechanics is inexpensive. 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 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 flow is then of course the other way around. Position in Fig. Second

In the collecting containers 7, which are separate for all chambers 5a, 4 and 5b, there is new bulk material for the exchange of used adsorbent. It is important that during the adsorption of highly toxic substances and less aggressive media, the loaded adsorbent is separated. In the arrangement described, this is done simply by removing adsorbent layers corresponding to different adsorption fronts in separate collecting containers 25 and 26 (or in collecting containers of chambers 5a and 5b) and conveying them from there. Such 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 collecting container 25.

The exemplary embodiment shown in FIG. 3 differs from the exemplary embodiment according to FIG. 1 in that the distributor plates 8 'are arranged to rise from the inlet side to the outflow side of the reactor 1'. As a result, the blocking section 30 is extended while the adsorber 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 suitable openings to the interior of the reaction chamber 14 are formed in the discharge funnels 20, through which raw gas can enter, but no granular adsorbent can escape into the fluid inlet distributor. 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 wall 30 must be used can also be seen on the rear wall immediately above the bottom 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 collecting container 26 and the channel section 32 and serves to break up any caking in the individual funnels or in the execution tubes 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. In the housing 41 are two annular reaction chambers

44 and 45 arranged concentrically nested. In the exemplary embodiment described, the annular spaces 44 and 45 are filled with different adsorbents, for example the outer annular space 44 with HOK and the inner annular space with pelletized hard coal coke. Accordingly, the outer annular space 44 serves for the separation of the better adsorbable pollutants (corresponding to the first stage 4 of the previously described embodiment) and the inner annular space 45 for the NO reduction corresponding to the chambers 5 of the previously described exemplary embodiment. The first and second annular spaces 44 and 45 are each surrounded by annular fluid outlet channels 46 and 47. The fluid inlet 48 is also an annular channel which is arranged on the radially inner side of the annular space 44. The fluid inlet of the internal second reactor stage 45 is a central channel 49, which runs along the central axis 50 of the reactor 40. The annular fluid inlet 48 of the first reactor stage 44 and the likewise annular fluid outlet 47 of the second reactor stage

45 are cylindrical in the present case Partition 51 separated.

A helical inlet channel 52 is arranged in the head region of the reactor housing 41 coaxially around its central axis 50 and connected to the ring channel 48 serving as the fluid inlet of the first reaction stage 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 to the outside in the area above the pouring cones 37 and pushes between the feed hopper or tube 18, 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 stages 44 and 45 correspond to the relationships explained with reference to FIGS. 1 to 3. Due to the circular arrangement and subdivision of the distribution trays 8 and extraction trays 9, the funnels 18 and 20 preferably have a trapezoidal design, as can be seen from the left half of FIG. 5.

The design of the blinds or other separating elements for delimiting the reaction spaces 44 and 45 can also correspond to that of the exemplary embodiment described above, although the dividing walls 55 and 56 (or 65 and 66) on the inflow and outflow sides correspond to the chamber cross section have sufficient segmentation approximate circular design.

As already mentioned, the uncleaned fluid enters the reactor housing 41 through the inlet channel 52 which presses on a swirl, reaches the predominantly cylindrical inflow surfaces in the region of the separating elements 55, crosses the ring-shaped first reaction stage 44 and passes through on its outflow side the outflow-side separating elements 56 into the outer annular channel 46, is directed downward into a circular flow chamber 58 and flows there radially inward towards the central fluid inlet 49 of the second reaction stage 45. In the circular flow chamber 58, the fluid flows around the discharge funnels 20 and Discharge tubes 22 similar to the previously described embodiment.

In the central fluid inlet 49, the pollutants which have been adsorbed more rapidly are removed, i.e. Partially cleaned fluid is initially distributed axially 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 stage 45. The separating elements 65 separate the bulk material ring 45 on the inlet side and the separating elements 66 on the outlet side from the adjacent fluid channels 49 and 47. The outlet-side fluid channel 47 opens into a discharge funnel 59 in the head part, from where the clean gas can be passed into a centrally arranged chimney 60.

The inflow surface of the first reaction stage 44 corresponding to the separating elements 55 is approximately larger in radius than the inflow surface 65 of the second reaction stage 45. The flow velocity of the fluid in the first annular space is correspondingly smaller compared to that in the second annular space 45. This is also desirable, especially when the different adsorbents are used in the two annular spaces 44 and 45.

Annular storage chambers 61 and 62 are also arranged above the annular feed plates 8. A motor-driven distributor device in the form of a rotating rake 63 is arranged in or above the inner storage chamber 62. The rotating rake 63 levels the loading in the annular chamber 62. sensitive bulk goods even when fed through a single fixed feed nozzle 64.

The supply chamber 61 assigned to the first reaction stage 44 is fed with the aid of a rail wagon 67 through cover wall 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 space 44 and thus also in the storage space 61 can be compensated for in the loading space of the wagon 67, so that no flue gas can escape into the wagon and from there into the ambient atmosphere.

The invention is not limited to the illustrated Ausführungsbej games. It is therefore easily possible within the scope of the invention 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

, > -Claims

1. A method for separating undesired constituents from a fluid, in particular an exhaust gas, by adsorption on a lumpy or granular adsorbent, the exhaust gas to be treated flowing through at least one reaction space filled with adsorbent and passed through at least one adsorption layer, characterized in that Adsorbent is introduced into and separated from the reaction space through a plurality of separate feed and discharge funnels distributed in a grid pattern and that the fluid is passed partly from the side transversely to the adsorption layer and partly vertically through the reaction space in such a way that the adsorbent in takes part in the adsorption practically uniformly in all zones of the reaction space.

2. The method according to claim 1, characterized in that the fluid is partially introduced from above into the reaction space.

3. The method according to claim 1 or 2, characterized in that various undesirable fluid components, e.g. Hg, SO-, HC1 and NO are separated in different adsorption layers and removed from the reaction chamber in separate streams.

4. The method according to claim 3, characterized in that in at least two different adsorption layers unter¬ different adsorbents, for example hearth coke and hard coal activated coke are used.

5. The method according to claim 4, characterized in that the fluid flows through at least two different Adsorptionsschich¬ th with different flow rates.

-i? -

6. The method according to claim 5, characterized in that the same fluid stream is passed in succession through the Adsorptionsschich¬ th and the flow velocities are adjusted by dimensioning the Anström¬ surfaces assigned to the adsorption layers.

7. The method according to any one of claims 3 to 6, characterized ge indicates that the stripped Ad¬ sorbents are subjected to various further processing steps.

8. The method according to any one of claims 1 to 7, characterized ge indicates that the reaction space is filled and emptied in batches and that the fluid treatment takes place in at least one fixed bed.

9. The method according to any one of claims 1 to 8, characterized ge indicates that the discharge funnel and / or subsequent discharge pipes are washed with the fluid and heated.

10. Procedure. according to one of claims 1 to 9, characterized ge indicates that in a first adsorption layer heavy metals, in a second adsorption layer easily adsorbable gaseous components such as SO and HC1 are separated from the fluid and the fluid finally in a further one Reaction stage is subjected to a NO _χ reduction.

11. The method according to any one of claims 1 to 10, characterized ge indicates that part of the fluid is introduced from below through the Ad¬ sorbent discharge funnel into the reaction chamber.

12. Use of the method according to one of claims 1 to 11 for flue gas cleaning in waste incineration plants.

13. Device for separating undesired constituents from a fluid, in particular an exhaust gas, with a reactor (4) which delimits at least one reaction space (14), the feed means at the top and funnel-shaped take-off means at the bottom for the purpose and for the removal of a lumpy or granular adsorbent characterized in that the feed means are formed by a grid of several feed funnels (18) arranged side by side and one behind the other and the withdrawal means are formed by a further grid of feed funnels (20) arranged side by side and one behind the other and that both at least on one side as Fluid passages are also provided in the head region of the reaction space (14).

14. The apparatus according to claim 13, characterized in that the reaction space (14) by at least one row of separating elements (17, 16) in at least two substantially vertically and transversely to the fluid flow direction Reaktorabtei¬ le (40, 41) divided and that each reactor compartment has a plurality of feed and discharge funnels (20) with separately operable closure and / or metering devices (23, 27 and 24, 28).

15. The apparatus according to claim 14, characterized in that the separating elements are designed as blinds (16) or double blinds (17).

16. Device according to one of claims 13 to 15, characterized in that at least two separate reaction chambers (4, 5a, 5b; 40, 41), which can be filled and emptied independently of one another with adsorptive agents, spatially side by side -iβ- arranged and connected in series for the fluid flow.

17. Device according to one of claims 13 to 16, characterized in that the discharge funnel (20) and / or adjoining discharge pipes (21, 22) are arranged in the flow path (32) of the fluid to be cleaned.

18. The apparatus according to claim 13, 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 - Tubes (21, 22) are flushed by the fluid with heating.

19. Device according to one of claims 13 to 18, characterized in that the funnel grid (20) on the foot side is provided with openings for the passage of the fluid to be cleaned and that the openings are connected to the fluid inlet (2).

20. Device according to one of claims 13 to 19, characterized in that the fluid inlet (2) extends approximately over the entire height of the reaction space, while the fluid outlet ⁽ 31) only a limited height of the outlet side of the reactor ( 4) spanned to avoid flow short-circuits in the head area of the reaction space.

21. The apparatus according to claim 18, characterized in that a first reactor stage (4) is flanked on both sides by second Reaktorstu¬ fen (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). - £ 0-

22. Device according to one of claims 13 to 21, characterized in that a plurality of rows (18 ') of feed funnels (18) from the fluid inlet (2) are arranged one behind the other in stepped heights.

23. Device for separating undesired constituents from a fluid, in particular an exhaust gas, with a reactor (40) which delimits at least one reaction space (44, 45), the feed means on the head side and funnel-shaped draw-off means on the bottom for the purpose and for the removal of a lumpy or granular adsorbent has, in particular according to one of claims 13 to 20, characterized in that at least two annular reaction spaces (44, 45) are arranged concentrically in a cylindrical housing (41), that the two annular spaces (44, 45) for the fluid flow in

Are connected in series and that the inflow surfaces of the first for the fluid flow

Annulus (44) are larger than that of the second annulus (45).

24. The device according to claim 23, characterized in that the annular spaces (44, 45) are nested concentrically one inside the other.

25. The apparatus of claim 23 or 24, characterized gekenn¬ characterized in that the inflow and outflow surfaces of the two annular spaces (44, 45) are arranged so that the annular spaces substantially radially, preferably from the inside to the outside of fluid are flowed through.

26. The apparatus according to claim 25, characterized in that - 1/-

the first and second annular spaces (44, 45) are surrounded by annular fluid outlet channels (46, 47), that the fluid inlet for the first annular space (44) is also designed as an annular channel (48) and that the fluid inlet (48) of the first annular space≤ and the fluid outlet (47) of the second annular space (45) are separated by a cylindrical partition (51).

27. The apparatus according to claim 26, characterized in that the fluid outlet of the first annular space (44) forming Ringka¬ channel (46) is limited by the outer wall of the reactor.

28. The device according to one of claims 23 to 27, characterized in that a circular flow chamber (58) which connects the fluid outlet (46) of the first annular space (44) with the fluid inlet (49) of the second annular space (45), among which Discharge trays (9) are arranged such that the discharge funnel (20) and / or discharge pipes (22) are flushed and heated by the partially cleaned fluid flowing radially inwards from the outside.

29. Device according to one of claims 23 to 28, 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 space (44) connected is.

30. Device according to one of claims 23 to 29, characterized in that the feed (8) and discharge trays (9) ring-shaped and the funnel (18, 20) are trapezoidal.

31. Device according to one of claims 23 to 30, characterized in that annular storage chambers (61, 62) are arranged above the annular feed trays (8). -02-

32. Apparatus according to claim 31, characterized in that a motor-driven circumferential distribution device (63) is mounted on an axis of rotation coinciding with the vertical housing axis (50) in an annular storage chamber (62).

33. Apparatus according to claim 31 or 32, characterized gekenn¬ characterized in that in a top wall of an annular Vorratskam¬ mer (61) uniform loading openings (68) are arranged at the same distance around the housing axis (50) and that a rail ring (69) is arranged at a corresponding radial distance above the top wall.

34. Apparatus according to claim 33, characterized in that a rail vehicle (67) running on the rail collar (69) with means for preferably airtight docking at the loading openings (68), an airtight lockable loading space and a blower for pressurizing the loading ¬ room is provided.