WO1987003214A1 - Procede d'elimination simultanee de matieres toxiques contenues dans des gaz de fumee et reacteur pour l'application du procede - Google Patents

Procede d'elimination simultanee de matieres toxiques contenues dans des gaz de fumee et reacteur pour l'application du procede Download PDF

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Publication number
WO1987003214A1
WO1987003214A1 PCT/DE1986/000479 DE8600479W WO8703214A1 WO 1987003214 A1 WO1987003214 A1 WO 1987003214A1 DE 8600479 W DE8600479 W DE 8600479W WO 8703214 A1 WO8703214 A1 WO 8703214A1
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Prior art keywords
reactor
flue gas
additive
container
screw
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PCT/DE1986/000479
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German (de)
English (en)
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Lothar Müller
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    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/48—Sulfur compounds
    • B01D53/50—Sulfur oxides
    • B01D53/508—Sulfur oxides by treating the gases with solids
    • 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
    • B01D53/34—Chemical or biological purification of waste 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/54—Nitrogen compounds
    • B01D53/56—Nitrogen oxides
    • 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
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/46—Removing components of defined structure
    • B01D53/68—Halogens or halogen compounds

Definitions

  • the invention relates to a process for pollutant supply from flue gases by adding a fine-grained, pollutant-binding, solid additive to the flue gas abströmsei term of the steam donkey, partial implementation of the additive with the pollutants contained in the flue gas stream with multiple changes in the direction of flow of the additive Flue gas in a reactor and separation of the additive from the flue gas behind the reactor and then in a filter.
  • the invention also relates to a reactor for carrying out this process, which has a cylindrical container with inlet and outlet connections for the flue gas, central m-i t assemblies equipped with a drivable shaft and internals projecting from the container wall.
  • the pollutant-forming, powdery additive is made from e.g. Kal hydrate, calcium carbonate, magnesium oxide or the like. e.g. mixed with the flue gas in a mixing nozzle and separated from the flue gas after a certain stretch.
  • the contact time between additive and flue gas is relatively short and the conversion of the additive and the degree of desulfurization of the flue gas are correspondingly low. This is of the order of 45%.
  • the invention has for its object to provide a method for removing pollutants from flue gases and denitrification, which is characterized by an increased use of the additive. Furthermore, a process for dry flue gas desulfurization is to be created, in which one . compared to known dry pollutant removal process increased pollutant removal from the flue gas is achieved. In addition, a flue gas pollutant removal reactor is also to be created, which enables an increased residence time of coarser additive particles in the flue gas and a higher relative speed of these particles in the flue gas stream. Finally, the reactivity to gross and / od agglomerated additive particles can be increased in the reactor '.
  • the recycling of the separated fraction into the flue gas stream to be desulfurized or the reactor therefore enables a considerable increase in the additive conversion or utilization overall without the reactor having to be burdened again with the already largely converted fine fraction of the additive.
  • the pollutant reduction in flue gases in the reactor is improved to about 80% or more and brought to the filter over 90% .
  • other environmentally harmful flue gas contaminants such as N0 X , SO3, HC1, HF will also be removed from the gas.
  • the fly ash contained in the recycled additive supports the ad- / absorption of the flue gas contaminants.
  • the speed of the flue gas stream is reduced before leaving the reactor and the coarser additive fraction is thereby separated from the gas stream.
  • the finer additive fraction is discharged from the reactor with the flue gas stream and separated from the gas stream in a downstream cyclo separator up to about the stoichiometrically required value.
  • the separation of the coarse fraction a the flue gas stream in the reactor can be supported by single or multiple deflection of the gas stream on this section of slowed speed.
  • the fraction withdrawn from the reactor and separating cyclone is comminuted into a flue gas flowing to the reactor, the partial flue gas is loaded with the comminuted and reactivated additive fraction and this flue gas stream 1 is combined with the other Part of the flue gas to be cleaned.
  • This comminution of the recycled fraction increases the reactivity of this fraction, since unreacted additive is exposed on the inside of the grain and becomes accessible for implementation
  • fresh additive and, if appropriate, part of the fine fraction of the additive separated off in the filter can also be comminuted and fed back to the reactor. In this way, a mixture of the comminuted coarse fraction of the additive with fresh additive is achieved. Part of the fine fraction from the downstream filter will only be returned in special cases, for example during the start-up period, since this portion - as explained above - has already been largely used. As will be explained below, it is up to the operator to increase or decrease the coarse fraction separated in the reactor and cyclone separator, so that he achieves the desired ratio of recycled to fresh additive without the aid of fine fraction from the filter . Grinding can take place in a classifier mill. The recycled fraction is expediently ground to a fineness of 20-5 ⁇ .
  • the weight ratio of the recycled additive to the fresh additive introduced into the reactor is preferably selected in the range from 3: 1 to 30: 1, in particular in the range from 5: 1 to 20: 1. A typical weight ratio is around 10: 1.
  • the high recycle ratio is based on the still relatively high reactivity of the comminuted recycled fraction and leads to a high additive concentration in the flue gas in the reactor, which in turn is favorable for a high pollutant binding.
  • the flue gas to be cleaned is brought into contact with an amount of additive which is approximately 10 to 30 times the amount stoichiometrically required for binding all bindable pollutants.
  • the temperature in the reactor is expediently kept in the range from 140 to 230.degree. C.
  • the heat exchanger is preferably arranged between the filter system and the chimney. However, it can also be arranged between the reactor and the filter system in order to be able to use cheaper filter fabrics.
  • the heat recovery rate from the flue gas is in the range of 25 to 45%.
  • the reactor for carrying out the process consists of a cylindrical container with inlet and outlet ports for the flue gas, a central shaft which can be driven and is fitted with superstructures, and internally projecting internals.
  • the reactor is characterized in that a flow channel connecting the two nozzles is formed in the vessel by the vessel internals or the shaft superstructures, which flow channel has an enlarged flow cross-section in the vicinity of the outlet nozzle, and the Container in the area with an enlarged flow channel cross section is equipped with a discharge device for the deposited additive.
  • a helical flow channel with its entire Long constant.
  • Flow cross-section of the reactor according to the invention has a cross-sectional expansion in the area near the outlet, which generally makes up t / 5 to 2/5 of the reactor height, so that in this area a reduction in the flow rate of the flue gas and thus a separation * of the coarse fraction of the additive occurs.
  • the discharge device is arranged so that the coarse fraction deposited in the reactor can be removed continuously or discontinuously from the reactor without the outflow of the flue gas laden with fine fraction being impaired in any way.
  • the outlet port for the flue gas is a piece, for example 30 to 70 cm above the bottom of the container, on which the coarse fraction of the additive collects, so that entrainment of coarse parts is avoided by the outlet port.
  • the vessel internals are designed as guide plates which are perpendicular to the shaft, are fixedly attached to the vessel wall at a mutual spacing and are provided with offset openings and have a greater mutual spacing in the region near the gas outlet nozzle than in the rest of the vessel or completely absent, and furthermore the shaft structures are designed as arms and, if necessary, arms that sweep over the container wall.
  • the diagonal displacement in particular - the opening in the guide plates the flue gas flows back and forth through the reactor from top to bottom or from bottom to top.
  • the gas flow slows down and the coarse fraction separates, which in turn is deposited on the discharge floor.
  • the coarser portions of the additive settle on the guide plates after the impact against the reactor wall.
  • the additive particles are again picked up by the flue gas stream and accelerated horizontally, there being a relative speed between the particles and the flue gas stream which is favorable for the mass transport on the particle surface and thus for the further reaction of the particle with pollutants. Due to its size, the particle can in turn settle on the next lower level.
  • the process described is repeated a number of times in the reactor, as a result of which the residence time of the particles in the reactor is considerably greater than the residence time of the flue gas, which is likewise advantageous for a thorough reaction.
  • the additive particle is deflected by 180 ° during the transition from one floor to the next lower one, particularly agglomerated additive particles are thrown against the outer wall of the reactor and thereby broken, or lose their outer layer, and thereby become more reactive again.
  • the construction with the fixed guide plates and rotating scraper arms is particularly suitable for reactors with a larger diameter and is favored.
  • the shaft structures are designed as a screw that extends essentially to the cylindrical container wall, which has a greater pitch in the area near the gas outlet nozzle than in the rest of the container or is completely absent.
  • the channel through which the flue gas flows is formed by the helical screw flights, the slowing down of the speed of the flue gas in the region near the outlet being brought about by the larger pitch or the lack of the screw.
  • the pressure loss of this reactor is lower than in the above-mentioned reactor with several fixed guide plates, but the production of the screw is more expensive with a larger reactor diameter.
  • the container internals as from the container wall projecting essentially radially inwards, vertically displaceable, with scrapers, brushes or the like.
  • arms attached to the snail and the screw can be provided with radial slots which are spaced apart from one another by a screw pitch.
  • the arms equipped with m scrapers or brushes are raised by an incline of the worm during operation of the reactor by the rotating worm over the worm plate and then fall again by an incline through the radial slots of the worm.
  • the vertically guided arms which are in pairs on the top and bottom of the screw and are mounted on the outside of the container wall, project through vertical slots in the container wall into the inside of the container. This paired arrangement of the arms cleans both sides of the screw, ie the top and bottom. Since each arm cleans only one screw pitch, the reactor contains as many cleaning arms as the screw has slopes.
  • the pressure of the cleaning arms on the screw surfaces and the falling speed of the cleaning arms can be regulated by counterweights attached on the outside.
  • This cleaning principle can also be applied when the screw rotates in the opposite direction: the cleaning arms are then pushed down by the screw against the force of an external counterweight and lifted back up through the slots by the slots after passing through a slope through the outer counterweights.
  • the cleaning arms can be guided on vertical columns on the outside of the container wall.
  • the shaft structures in particular the worm, are expediently serrated or interrupted in some other way at their outer edges that come into contact with the additive attached.
  • the friction between the edges of the shaft structures and the inside of the reactor wall, on which solid material from the flue gas has accumulated, is reduced and the scraping off of these approaches is facilitated.
  • the shaft assemblies expediently also have arms with guide vanes directed obliquely inwards.
  • the additive contained in high concentration in the flue gas is di Centrifugal raft compresses in the outer area of the helical channel and thereby affects the contact between additive and flue gas.
  • the guide vanes convey this additive, which has been compressed in the edge region, back inwards and thus ensure an intensive, uniform mixing of the additive with the flue gas stream.
  • the impact of large or agglomerated additive granules simultaneously reduces them, which has a favorable effect on the reactivity of the material in the reactor.
  • the flue gas outlet connection is shielded by a deflecting screen.
  • the deflecting screen at the outlet nozzle also has the task of separating the coarse portion of the additive from the flue gas stream.
  • the separating effect of the screen can be changed by its adjustable size, so that the portion separated in the reactor can be changed within limits.
  • the deflecting screen is expediently attached to the container wall.
  • the shaft structures are preferably in the area near the gas outlet connection than with scrapers, brushes or the like. equipped arms designed to sweep over the container wall and / or the deflecting screen. These arms prevent the coarse-grained additive from being deposited on the surfaces which are not covered by the discharge device.
  • the discharge device can attached to the shaft consist of one, the container bottom sweeping wiper arm, an "opening in the vessel bottom and attached to the opening of feed line.
  • the settled on the tank bottom coarse fraction of the additive by the rotating Abstreiferar in diez.B. as a radial slot The material then falls into the conveyor line, through which it is preferably fed to a comminution device, for example the above-mentioned classifier mill.
  • the conveyor line can be, for example, a screw conveyor or a pneumatic conveyor system Flue gas bypass stream removed
  • the pneumatic delivery line is, for example, through a Cell wheel lock separated from the interior of the reactor.
  • the discharged coarse fraction can also be fed to the grinding plant or the device for feeding into the flue gas stream by other means of transport.
  • This impact can be supported by redirecting in the reactor e.g. by installing one or more driven impact beater mills in the area of the deflection, FIGS. 9 and 10.
  • Zone 1 Dick Stroni Zones
  • pollutants such as SO?, HF, HC1, etc.
  • Low-pollutant flue gas with little additive is located behind the reactor and the cyclone separator which may be connected downstream. In this condition, quantitative denitrification is only possible with limited chemically negative side effects with Na (OH) or NH3. Na (OH) gives more stable connections, no odor nuisance and is cheaper.
  • 3rd zone dedusting and after-reaction in the fabric filter
  • the additive loading compared to all known methods, is only slightly above the stoichiometric value.
  • the now very small amount of additive can be accumulated somewhat through the reduced cleaning intensity of the filter bags in order to achieve a more intensive after-reaction.
  • the reactor is expediently thermally insulated and provided with additional heating.
  • the thermal insulation prevents the temperature from falling below the dew point, in particular when the system is started up, and the utilization of the heat of the cleaned flue gas in the downstream heat exchanger is improved.
  • An additional jacket heating of the reactor is of advantage to avoid falling below the dew point during the start-up period.
  • FIG. 1 shows a schematic flow diagram of a plant for carrying out a first embodiment of the method according to the invention
  • FIG. 2 shows an apparatus flow diagram of a plant for carrying out a second embodiment of the method according to the invention using a first embodiment of a reactor;
  • Figure 4 shows a section along the line IV - IV of Figure 3 in a simplified representation
  • FIG. 5 shows a schematic axial section of a second embodiment of the reactor according to the invention.
  • FIG. 6 shows a schematic axial section of a third embodiment of the reactor according to the invention.
  • Figure 8 is a partial view of the system shown in Figure 1 in detailed form
  • Figure 9 is a schematic axial section. a fourth embodiment of the reactor according to the invention.
  • FIG. 10 shows a section along the line X - X, FIG. 9.
  • a little H 0 is added to the flue gas coming from the boiler system and then fed through line 1 to a reactor 2.
  • Part of the flue gas is passed through the bypass line 3 via a classifier or other mill 4 which is fed via line 5 with a mixture of fresh additive supplied by line and partially converted coarse fraction of the additive returned through line 7.
  • the bypass stream loaded with the ground additive is recombined with the main stream of the flue gas in line 1.
  • the reaction between the additive and the pollutants contained in the flue gas essentially takes place in the reactor 2.
  • the fraction of the partially converted additive is separated. The one behind the reactor
  • Line 11 is discharged and eliminated. If desired, part of this material can also be fed through line 12 into the
  • the flue gas to be sulfurized in line 1 through the feed nozzle 13 on the one hand the additive and on the other hand water is added.
  • the fresh additive is introduced from a silo 14 via the cell lock into a screw 15 which conveys the additive into the nozzle 13.
  • coarse, partially converted addi is fed into the conveyor screw 16 through the return line 7, which is equipped with a screw b, and is thus fed back to the flue gas flow through the nozzle 13.
  • the reactor 2 shown in FIG. 2 has a container made of cylindrical wall 17, container bottom 18 and container lid 19.
  • a vertical, axia shaft 20 is housed, which is mounted on the bottom 18 and cover 19 and is driven by a motor 21.
  • the shaft 20 carries a worm 22, the edge of which is at a short distance from the container wall 17.
  • the shaft 20 also carries arms 26 with guide vanes 27, the inclination of which can be seen in FIG. 3.
  • the slope of the screw 22 is greater in the lower part of the reactor than in the upper (y - x), so that in the lower part of the reactor the flow velocity is slowed down and thus coarse and / or agglomerated additive and fly ash particles are deposited on the bottom 18.
  • the shaft 20 also carries a scraper arm 28 grazing the bottom 18, which conveys the separated bulk material to the bottom opening 29, through which it falls into the delivery line 30, which is connected via a row wheel lock 3 to the return line 7.
  • the flue gas leaving the reactor 2 through the outlet port 24 is also passed via a cyclone separator with an adjustable immersion tube through line 8 into the bag filter system 9, where the additive still contained in the flue gas is completely discharged, the flue gas being discharged as it flows through the filters different additive layer comes into intensive contact with the additive and there is still an after-reaction.
  • the cleaned flue gas possibly leaves the filter system via e heat exchanger through line 10 and is conveyed to the chimney by the fan.
  • the additive material deposited in the filter system is discharged through the screw 33 and e is not eliminated either through line 11 or in special cases, .z when the additive loading of the smoke in the reactor is still too low when the system is started up, via a cell wheel lock 34 and return line 12 fed to line 7.
  • the arrangement of the arms 26 with the inclined guide vanes 2 can be seen from FIG.
  • the blades 27 have the task of guiding the additive particles concentrated in the helical flow channel 25 under the action of the centrifugal force towards the container wall 17 back into the flow and thus ensuring better contact between the gas and the solid additive, as can also be seen in FIG. 3 is, the screw 22, only partially shown, has a radial slot 35 and one serrated edge 36.
  • the serrated edge 36 reduces the friction on the container wall 17.
  • the container wall 17 has a slot 37 through which an arm 38, for example equipped with brushes (not shown), projects radially into the interior of the reactor and with its brushes rests against the top of the screw.
  • an arm 38 for example equipped with brushes (not shown)
  • the arms 38 are arranged in pairs such that one arm engages with the top and the other arm with the bottom of the screw 22. There is such a pair of arms in each worm gear. All pairs of arms are in a closed extension 39 outside of the container jacket 17 vertically displaceable I position In order to hold and slidably support the pairs of arms, two vertical columns 40 are provided in the extension 39.
  • the shaft 20 rotates, the worms 22 cleaning the upper and lower arms 38 are raised until they reach the slot 3.
  • the upper arm 38 then falls through the slot 35 and hits - since the shaft 20 has rotated a little further during the fall - onto the worm gear underneath, while the lower arm 38 passes through the lower slot 35 and in turn cleans the underside of the worm plate
  • the embodiment of the reactor shown in FIG. 5 differs from the reactor shown in FIG. 2 essentially in that the screw 22 does not extend over the entire height of the reactor, but rather the lower third is free of screws. After leaving the helical flow channel 25, the flue gas therefore slows down its flow rate, so that the coarse additive particles can settle on the container bottom 18.
  • a deflecting screen 41 is arranged on the container wall 17 above the outlet port 24, which consists of a fixed part and a part (not shown) which can be moved on it, so that the flue gas flow is in front Exit from the connection piece is deflected to a greater or lesser extent depending on the position of the displaceable part, and the proportion of the additive separated in the reactor 2 can thereby be varied within limits.
  • the shaft 20 carries arms 42 which are equipped with scrapers 43, brushes or the like in order to clean the container wall in this area and the deflecting screen 41.
  • the discharge device 28-30 is essentially the same as in the reactor according to FIG. 2 .
  • the reactor shown in FIG. 6 differs from the reactors of FIGS. 2 to 5 essentially by the F of the flow channel 25, which is not of helical design but rather a reciprocating course with U deflections of the gas flow of 180 "in each case.
  • the cylindrical container jacket 17 is inserted into the guide plates 44, which are perpendicular to the container axis, each guide plate 44 has an opening 45, the openings 45 of adjacent guide blocks being diagonally opposite one another, and all guide plates 44 have the same distance from the adjacent guide plates, so that the flue gas In the lower third of the reactor there are no guide plates, so that the flow cross-section widens here, the flow velocity slows down and the coarse-grained additive settles out of the gas stream 46 attached to the Lei tb ⁇ den 44 stripped additive from the floors and d throws the openings 45 in the flue gas stream on the next floor.
  • the particles can then be bombarded by the gas stream and carried away or can be deposited on the next lower guide floor 44 again.
  • the dwell time of at least the coarser-grained additive in the reactor can be extended considerably and can also be varied accordingly by the shaft speed. Since the flue gas stream changes direction by 180 ° at the transition from one floor to the next, large additive particles and agglomerates meet the container jacket 17 and are at least partially crushed. This no longer creates coated additives, which are activated again and taken away by the flue gas stream. This classifying effect of the reactor is desirable since finer additive particles also react quickly and further than agglomerates.
  • the lower third of this reactor does not differ significantly from the embodiment according to FIG. 5.
  • the deflecting screen 41 runs essentially horizontally.
  • the connectors 23, 24 are attached centrally to the jacket 17, while at least the inlet connector 23 is attached tangentially to the reactor with a helical flow path.
  • the shape of the opening 45 shown in FIG. 7 is to be understood as an example. The opening can of course have a different shape.
  • FIG. 8 shows the return of the fraction of the additive separated off in the reactor 2 via a mill 4 into the flue gas of line 1 in accordance with the method shown in FIG. 1.
  • the fraction returned through line 7 and fresh additive from the silo 14 are fed through the conveyor screw 16 into the mill 4 and are comminuted there in the flue gas partial stream supplied through the bypass line 3.
  • Only the grain size that can be set, in the present case e.g. material reduced to a grain size d ⁇ 20 to 5 ⁇ m is taken from the flue gas part 1 and fed pneumatically via the blower 47 and the bypass line 3 to the main flue gas flow in line 1.
  • FIG. 9 corresponds essentially to the reactor shown in FIG. 6 % and differs only in that
  • FIG. 10 shows a section of the reactor according to FIG. 9 in the area of the 180 ° deflection.
  • the method according to the invention and the reactor for carrying out the method can also be used for very small amounts of flue gas, such as those that occur in domestic combustion systems (including Ulfe systems).
  • the present invention also includes embodiments of the method in which the coarser additive fraction is separated from the flue gas stream upstream of the filter.
  • This separate separation of the coarse fraction can, for example, only take place in a Z y k lon or in an additional filter.

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Abstract

Selon ce procédé, des quantités multiples, stoechiométriquement déterminées, d'un additif solide à grains fins se liant aux matières toxiques sont introduites dans le gaz de fumée en aval de l'installation de chauffe. L'additif est partiellement transformé avec les matières toxiques contenues dans le gaz de fumée pendant que le sens d'écoulement du gaz de fumée chargé d'additif se modifie plusieurs fois dans le réacteur, à nouveau précipité, puis l'additif restant est séparé du gaz de fumée par un filtre. Le procédé se caractérise par le fait que l'on sépare une certaine proportion de l'additif du courant de gaz de fumée dans le réacteur ou en aval de celui-ci, mais en tout cas avant le filtre, et qu'on le réintroduit, après fragmentation, dans le courant de gaz de fumée entre la chaudière et le réacteur ou après son entrée dans le réacteur. Ce procédé permet de mieux utiliser l'additif et d'éliminer davantage de matières toxiques contenues dans le gaz de fumée.
PCT/DE1986/000479 1985-11-26 1986-11-25 Procede d'elimination simultanee de matieres toxiques contenues dans des gaz de fumee et reacteur pour l'application du procede Ceased WO1987003214A1 (fr)

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Application Number Priority Date Filing Date Title
DE3541729 1985-11-26
DEP3541729.3 1985-11-26

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WO1987003214A1 true WO1987003214A1 (fr) 1987-06-04

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Cited By (2)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998041309A1 (fr) * 1997-03-19 1998-09-24 Schneider, Wolfgang Procede d'elimination de substances nocives acides contenues dans des effluents gazeux
DE202019000538U1 (de) 2019-02-05 2019-05-09 Vesch Technologies GmbH Entstaubungsanlage

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Publication number Priority date Publication date Assignee Title
US2600871A (en) * 1949-06-27 1952-06-17 Gulf Research Development Co Continuous conveyer-reactor chamber
DE2437750A1 (de) * 1974-08-06 1976-02-26 Huenlich Hans Werner Dipl Ing Ein- und mehrstufiges verfahren zur trockenen absorption und abscheidung gasfoermiger schadstoffe aus abgasen als trockene rueckstaende
DE3001525A1 (de) * 1980-01-17 1981-07-23 Adolf Dipl.-Ing. 3060 Stadthagen Margraf Vorrichtung zum stoffaustausch in einer wirbelschichtkammer
DE3041997A1 (de) * 1980-11-07 1982-06-09 Friedrich 4983 Kirchlengern Hellmich Verfahren zur abtrennung von umweltschaedigenden gasen aus rauchgasen, insbesondere von tunneloefen, und vorrichtung zur durchfuehrung des verfahrens
DE3311100A1 (de) * 1983-03-26 1984-09-27 Wolf Dr.-Ing. 7573 Sinzheim Schulteß Neues verfahren zur gasreinigung - akitvierungssorption

Patent Citations (5)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US2600871A (en) * 1949-06-27 1952-06-17 Gulf Research Development Co Continuous conveyer-reactor chamber
DE2437750A1 (de) * 1974-08-06 1976-02-26 Huenlich Hans Werner Dipl Ing Ein- und mehrstufiges verfahren zur trockenen absorption und abscheidung gasfoermiger schadstoffe aus abgasen als trockene rueckstaende
DE3001525A1 (de) * 1980-01-17 1981-07-23 Adolf Dipl.-Ing. 3060 Stadthagen Margraf Vorrichtung zum stoffaustausch in einer wirbelschichtkammer
DE3041997A1 (de) * 1980-11-07 1982-06-09 Friedrich 4983 Kirchlengern Hellmich Verfahren zur abtrennung von umweltschaedigenden gasen aus rauchgasen, insbesondere von tunneloefen, und vorrichtung zur durchfuehrung des verfahrens
DE3311100A1 (de) * 1983-03-26 1984-09-27 Wolf Dr.-Ing. 7573 Sinzheim Schulteß Neues verfahren zur gasreinigung - akitvierungssorption

Cited By (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO1998041309A1 (fr) * 1997-03-19 1998-09-24 Schneider, Wolfgang Procede d'elimination de substances nocives acides contenues dans des effluents gazeux
DE202019000538U1 (de) 2019-02-05 2019-05-09 Vesch Technologies GmbH Entstaubungsanlage
WO2020160837A1 (fr) 2019-02-05 2020-08-13 Vesch Technologies GmbH Procédé pour changer un filtre et système de dépoussiérage

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