WO1996004065A1 - Reacteur a adsorption utilise pour extraire les composants indesirables d'un fluide - Google Patents

Reacteur a adsorption utilise pour extraire les composants indesirables d'un fluide Download PDF

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Publication number
WO1996004065A1
WO1996004065A1 PCT/EP1995/002725 EP9502725W WO9604065A1 WO 1996004065 A1 WO1996004065 A1 WO 1996004065A1 EP 9502725 W EP9502725 W EP 9502725W WO 9604065 A1 WO9604065 A1 WO 9604065A1
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WO
WIPO (PCT)
Prior art keywords
fluid
reactor according
adsorption reactor
discharge
feed
Prior art date
Application number
PCT/EP1995/002725
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German (de)
English (en)
Inventor
Hermann BRÜGGENDICK
Original Assignee
Steag Aktiengesellschaft
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
Filing date
Publication date
Priority claimed from DE19518448A external-priority patent/DE19518448B4/de
Application filed by Steag Aktiengesellschaft filed Critical Steag Aktiengesellschaft
Priority to JP8506121A priority Critical patent/JP3068856B2/ja
Priority to CA002196217A priority patent/CA2196217C/fr
Priority to TW084107723A priority patent/TW315309B/zh
Publication of WO1996004065A1 publication Critical patent/WO1996004065A1/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/06—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds
    • B01D53/08—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with moving adsorbents, e.g. rotating beds according to the "moving bed" method
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
    • B01J8/125—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow with multiple sections one above the other separated by distribution aids, e.g. reaction and regeneration sections
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2253/00—Adsorbents used in seperation treatment of gases and vapours
    • B01D2253/10—Inorganic adsorbents
    • B01D2253/102—Carbon
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/204—Inorganic halogen compounds
    • B01D2257/2045—Hydrochloric acid
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/20—Halogens or halogen compounds
    • B01D2257/206—Organic halogen compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/30—Sulfur compounds
    • B01D2257/302—Sulfur oxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/40—Nitrogen compounds
    • B01D2257/404—Nitrogen oxides other than dinitrogen oxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/60—Heavy metals or heavy metal compounds
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/02—Other waste gases
    • B01D2258/0283—Flue gases
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/02—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography
    • B01D53/04—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by adsorption, e.g. preparative gas chromatography with stationary adsorbents
    • B01D53/0407—Constructional details of adsorbing systems
    • B01D53/0431—Beds with radial gas flow

Definitions

  • 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.
  • the exhaust gas should be cleaned as far as possible, since the exhaust gas is still offered sufficient fresh adsorbent 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.
  • 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.
  • 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.
  • 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.
  • the adsorbent streams loaded with particularly fast-reacting heavy metals, for example mercury or also organic substances, are disposed of separately.
  • adsorbents loaded with SO2 and HCl so-called hearth furnace coke (HOK) is sufficient as adsorbent, that is lignite activated coke, the regeneration of which is uneconomical.
  • HOK hearth furnace coke
  • pelleted hard coal activated coke is preferred as the adsorbent. Its price makes recycling and reuse in a NOx reduction stage economically viable.
  • 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.
  • 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.
  • 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 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.
  • 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.
  • 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
  • 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.
  • a matrix-like arrangement of the discharge funnels is used.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • the Venetian blind slats preferably have different directions of inclination.
  • the blind slats 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.
  • the slats, starting from the strip profiles are inclined upwards, preferably at an angle of approximately 25 to 35 ° to the vertical plane.
  • 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 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.
  • 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
  • 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.
  • 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.
  • 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.
  • 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 .
  • FIG. 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;
  • FIG. 3 shows a view corresponding to FIG. 1 of a modified embodiment of the invention
  • FIG. 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;
  • FIG. 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.
  • the chamber 14 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.
  • 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 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.
  • 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.
  • 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.
  • NH3 is injected as a reducing agent at the deflection point between the outlet channel 31 and the horizontal channel section 32.
  • feed points or pre-loading of the hard coal activated coke in the chambers 5a and 5b are also possible.
  • 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.
  • other forms are possible with basically the same advantages of the invention.
  • inflow surfaces of the two reactor stages 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.
  • 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.
  • 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.
  • a cylindrical reactor housing 41 ' In the housing 41 'are two annular reaction chambers
  • 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
  • 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.
  • 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.
  • the fluid flows around the discharge funnels 20 and the exhaust pipes 22 similar to the previously described embodiment.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • the gas 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.
  • 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.
  • the reactor 101 has a rectangular cross section. It has a housing 102 which delimits a reaction chamber 103.
  • 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
  • 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.
  • 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.
  • 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).
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • 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.
  • highly toxic components such as dioxins and furans
  • 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.
  • both the gap limiting elements 113a and the strip profiles 116 running parallel to them is generally preferred for reasons of cost.
  • these vertically extending components 113a and 116 can, however, also be assembled from several parts either in abutment or with toothing or overlap.
  • 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.
  • 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.
  • 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.
  • 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 stabilizing grid is individually assigned to the slotted screen sections 151a ... 151c. 14 shows only the transverse connecting rods 155.
  • 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.

Abstract

Un réacteur comprend une chambre de réaction (103) qui est alimentée en milieu adsorbant par l'intermédiaire d'entonnoirs d'alimentation en forme de grille et qui est vidée par l'intermédiaire d'entonnoirs de décharge (106) en forme de grille. La chambre est délimitée par des obturateurs à lamelles (108, 109) et subdivisée en deux couches (103a, 103b) par une cloison (107). La cloison (107) et l'obturateur (108) se trouvant en aval ont sensiblement la même structure, c'est-à-dire un crible à fente en amont suivi d'une grille de stabilisation raccordée à des lamelles (120 ou 110) orientées vers le bas au niveau de la cloison (107) et vers le haut au niveau de l'obturateur (108). On peut assembler le réacteur de façon modulaire dans le sens longitudinal et dans le sens transversal à partir d'une pluralité de chambres de réaction.
PCT/EP1995/002725 1994-07-29 1995-07-12 Reacteur a adsorption utilise pour extraire les composants indesirables d'un fluide WO1996004065A1 (fr)

Priority Applications (3)

Application Number Priority Date Filing Date Title
JP8506121A JP3068856B2 (ja) 1994-07-29 1995-07-12 流体から望ましくない成分を分離するための吸着反応器
CA002196217A CA2196217C (fr) 1994-07-29 1995-07-12 Reacteur a adsorption utilise pour extraire les composants indesirables d'un fluide
TW084107723A TW315309B (fr) 1994-07-29 1995-07-25

Applications Claiming Priority (4)

Application Number Priority Date Filing Date Title
DEP4426895.5 1994-07-29
DE4426895 1994-07-29
DE19518448A DE19518448B4 (de) 1994-11-29 1995-05-19 Verfahren und Vorrichtung zum Reinigen eines Fluids
DE19518448.3 1995-05-19

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WO1996004065A1 true WO1996004065A1 (fr) 1996-02-15

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Cited By (4)

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DE19856736A1 (de) * 1998-12-09 2000-06-15 Wilhelm Wollner Verfahren und Vorrichtung zur kurzzeitigen und energiesparenden Erhitzung von granulatförmigen Stoffen
WO2008031535A1 (fr) * 2006-09-14 2008-03-20 Haldor Topsøe A/S Procédé de production d'acide sulfurique
AT520534B1 (de) * 2018-04-19 2019-05-15 Andritz Ag Maschf Anlage zur Absorption von Einzelkomponenten aus Gasen
CN113209767A (zh) * 2021-05-28 2021-08-06 沈阳东大山汇环境科技有限公司 一种物理阻隔吸附气-液-固分离装置及方法

Families Citing this family (2)

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US9048508B2 (en) 2007-04-20 2015-06-02 Mitsubishi Chemical Corporation Nonaqueous electrolytes and nonaqueous-electrolyte secondary batteries employing the same
CN111121050B (zh) * 2019-11-29 2020-08-25 湖州森诺环境科技有限公司 一种垃圾飞灰除二噁英***及其处理方法

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DE4032738C1 (en) * 1990-10-16 1992-01-16 Steag Ag, 4300 Essen, De Adsorption agent esp. moving bed reactor - includes slot sieve downstream of bed and venetian blind type construction
WO1992006770A1 (fr) * 1990-10-16 1992-04-30 Steag Aktiengesellschaft Reacteur a milieu d'adsorption, notamment a lit fluidise
EP0533480A1 (fr) * 1991-09-18 1993-03-24 Mitsui Mining Company, Limited Procédé pour la désulfuration et la dénitration d'un gaz d'échappement contenant des matériaux halogènes

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GB2035128A (en) * 1978-11-24 1980-06-18 Rockwell International Corp Filtering apparatus and method
EP0198133A1 (fr) * 1985-04-15 1986-10-22 Mitsui Mining Company, Limited Réacteur à lit mobile contenant une jalousie principale et une jalousie supplémentaire
EP0213298A1 (fr) * 1985-07-24 1987-03-11 Kernforschungszentrum Karlsruhe Gmbh Dispositif pour supporter et guider des couches
EP0264669A1 (fr) * 1986-10-20 1988-04-27 H. Krantz GmbH & Co. Dispositif de logement de produits en vrac pouvant s'écouler
EP0376356A1 (fr) * 1988-12-30 1990-07-04 Steag Ag Méthode et procédé pour séparer des composants indésirables d'un gaz d'échappement
DE4032738C1 (en) * 1990-10-16 1992-01-16 Steag Ag, 4300 Essen, De Adsorption agent esp. moving bed reactor - includes slot sieve downstream of bed and venetian blind type construction
WO1992006770A1 (fr) * 1990-10-16 1992-04-30 Steag Aktiengesellschaft Reacteur a milieu d'adsorption, notamment a lit fluidise
EP0533480A1 (fr) * 1991-09-18 1993-03-24 Mitsui Mining Company, Limited Procédé pour la désulfuration et la dénitration d'un gaz d'échappement contenant des matériaux halogènes

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* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19856736A1 (de) * 1998-12-09 2000-06-15 Wilhelm Wollner Verfahren und Vorrichtung zur kurzzeitigen und energiesparenden Erhitzung von granulatförmigen Stoffen
WO2008031535A1 (fr) * 2006-09-14 2008-03-20 Haldor Topsøe A/S Procédé de production d'acide sulfurique
AT520534B1 (de) * 2018-04-19 2019-05-15 Andritz Ag Maschf Anlage zur Absorption von Einzelkomponenten aus Gasen
AT520534A4 (de) * 2018-04-19 2019-05-15 Andritz Ag Maschf Anlage zur Absorption von Einzelkomponenten aus Gasen
CN113209767A (zh) * 2021-05-28 2021-08-06 沈阳东大山汇环境科技有限公司 一种物理阻隔吸附气-液-固分离装置及方法
CN113209767B (zh) * 2021-05-28 2023-10-13 沈阳东大山汇环境科技有限公司 一种物理阻隔吸附气-液-固分离装置及方法

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JPH10503421A (ja) 1998-03-31
JP3068856B2 (ja) 2000-07-24
CA2196217C (fr) 2000-11-28
CA2196217A1 (fr) 1996-02-15

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