DE2615828A1 - Gas purificn. by addn. of absorbent - in series of stages with sepn. and recycling of absorbent after each stage - Google Patents

Abstract

A gas, at >=120 degrees C, requiring purificn. and to which can be added an oxidising agent, e.g. H2O2 or potassium permanganate, is passed through a series of tubes where it is mixed with an adsorption agent, e.g. slake lime, calcium carbonate, iron oxide, amorphous silica, porous perlite or filter carbon, having a granulometry pref. 50 mu. Each mixing tube is followed by a separator which removes the absorbant from the gas stream and recycles it counter-currently to the gas flow. Absorbant is introduced into each mixing tube through >=1 nozzle pointing downstream, each nozzle followed by a conical flow obstacle with its pointed end facing the nozzle, then a truncated converging section of the mixing tube reducing the flow area for the gas. Absorbant recycled counter-currently is removed from the separator after the first stage mixing tube, par of the absorbant is rejected and the rest is sent back to enter the final stage mixing tube, fresh make-up absorbant being added before it enters the mixing tube. Alternatively the recycled part of the absorbant is introduced into the penultimate mixing tube, with the fresh make-up absorbant being fed into the final mixing tube and the absorbant recovered from the separators after these stages is mixed before passing to the next mixing tube upstream. Rejected absorbant can be rid of harmful prods. by converting them to calcium sulphate using air and lime wash or by heating it in a Claus furnace after which it can be re-used. Process is used for purificn. of flue gases contg. SO2 and NOx. The absorbant need not be expensive and can be re-used several times with the process still giving a very high purificn. effect. The reaction is very rapid so that the installation is small and there is low energy usage.

Description

Method and device for gas cleaning

The invention relates to a method and a device for gas cleaning, especially for removing pollutants from exhaust gases, flue gases and useful gases.

To purify such gases, it is known that the gas with solid sorbents to bring into contact, which are separated again from the gas after sorption As far as the sorbents are in the immobile state in filters, wherein If the gas flows through these filters, the sorption is extremely slow in front of you. This has the consequence that the filters are extremely voluminous and that a very large amount of energy is required to force the gas through the filter will.

If, on the other hand, the gas is passed through a fluidized bed, the out granular sorbent, the cleaning effect is only marginal increases and energy consumption only slightly decreased, but it does occur Abrasion on the granular sorbent and the sorbent must very often to be renewed.

The known dry sorption processes for cleaning gases have In addition, the disadvantage that despite the very large construction volume of the systems only relatively small amounts of gas can be cleaned and a reasonably sufficient cleaning effect can only be achieved at gas temperatures in the range above 6000 C, whereby in turn, the construction and operation of the very large plants become extremely expensive.

The invention is based on the object of providing a method for gas purification, especially for the removal of pollutants from exhaust gases, flue gases and useful gases to create, in which a very high cleaning effect is achieved, that a very has rapid course of reaction, so that in a small plant under low Energy expenditure can be worked and at. which is an inexpensive sorbent can be used several times during a longer period of use.

The invention relates to a method for gas cleaning, in particular for the removal of pollutants from exhaust gases, flue gases and useful gases, in which the Gas brought into contact with solid sorbents and again after sorption is separated, which is characterized in that dust-like sorbents With the pollutants reacting substances are used in such a way that they are in the Introduced gas stream, guided with this through venturi sections and separated from the gas will.

It has surprisingly been found that such a intense turbulence between sorbent and gas can be achieved that the sorption reaction is extremely rapid. This is not the only reason possible in a structurally relatively small system very high Achieve relaxation therapy treatments Zll, but the procedure can also be completely significantly lower temperatures can be carried out than with the known Procedure is the case. Considerable energy savings can be achieved in this way achieve. On the other hand, the process can be filled with high temperatures not in the way, and this has the consequence that the gas to be cleaned is usually in that temperature point can be treated in which it arises. The procedure can be carried out at atmospheric or reduced as well as greatly increased pressure operate.

It can therefore be used, for example, for desulphurisation of natural gas use without it being necessary to reduce the natural pressure of the gas. The dusty sorbent is completely insensitive to mechanical stress. The inevitable reduction in size of the particles due to strong mechanical stress the sorbent is not. as in the case of the state of the art, negative, but an advantage.

It is therefore possible to re-use the sorbent separated from the gas To be introduced into the gas flow until the sorption capacity is exhausted or so reduced is that it is more economical to remove the sorbent and optionally to work up. This significantly increases the profitability of the Procedure allows.

In the preferred embodiment, the gas stream passes through several successive venturi sections, each with a separator for the sorbent is downstream and that the sorbent is first in the last of the gas flowed through Venturi section and then in the, against the direction of the gas flow seen, introduced subsequent Venturi routes. This results in though the Sorbents in the individual vnturistecn inevitably # Often in direct current with the gas is conducted, within the entire process a Gegess tromei: ft-kt that has a high degree of purification and is particularly economical Execution of the sorbent result.

When the sorbent is in circulation in the above manner is carried out, it is appropriate to determine the necessary condition of the sorbent by maintaining that the circulated sorbent part removed from the stream and added an appropriate amount of fresh sorbent is. The partial flow can be withdrawn behind the, seen in the direction of the gas flow, first venturi and the addition of fresh sorbent before heading towards of the gas flow seen last venturi. This results in a complete counterflow cycle of the sorbent.

In another embodiment of the method, the flax is the fresh one Sorbent first seen through the gas stream, last venturi out and only then in the sorbent circuit, which the preceding Venturi routes includes, initiated. By using only fresh sorbent in the last If necessary, venturi can also be stretched to very low residual concentrations remove pollutants from the gas.

Dust-like reactive compounds can be used as sorbents of alkali and / or alkaline earth metals can be used. Are particularly suitable Powdered hydrated lime and / or calcium carbonate, the latter preferably in the form of dolomite flour. Sulfur dioxide can be released through these sorbents nearly completely, hydrogen sulfide and nitrogen oxides very largely from the to be cleaned Remove gas.

Your cleaning effect can be improved by that the sorbent is dust-fine turf iron ore and / or powdered iron oxide, that is produced in steel production.

Dust can be used as a sorbent with particular advantage Use amorphous silicon dioxide, which is used in the electrothermal production of Ferrosilicon is obtained. This sorbent that with the pollutants chemically does not respond, can be easily regenerated and used again. When using it, there are no waste products, and their disposal is difficult could cause. Expanded perlites can be added to the sorbent, which also do not react chemically with the pollutants. You wise, as well like powdered amorphous silicon dioxide, good physical sorption properties and are also suitable for adding moisture to the reaction.

It is also possible to use filter carbon as a sorbent. These can be dust-like filters kohlea or dust-like ones Carbon, which is produced in the electrothermal production of carbon-metal compounds accrues The abovementioned sorbents can each be mixed individually be used. In any case, it is useful if the sorbent substantially Grain sizes below 100μ, preferably below 50 /.

However, a proportion of coarser grain that is not too large is harmless.

It is appropriate that the sorbent contains water.

When using hydrated lime as a sorbent this contains Material already has a certain amount of moisture, otherwise the sorbent can be moistened, whereby expanded perlite is particularly suitable as a carrier for moisture or water vapor can be added to the gas to be cleaned. Through the Presence of water, which is only added in such small amounts that the The flow of the sorbent can not be impaired, the course of the reaction can can be significantly accelerated, so that an improvement in the cleaning effect and an improved utilization of the sorbent is the result.

Especially if the gas to be cleaned contains N20 or other nitrogen oxides are present, it is expedient to remove the gas prior to contact with the sorbent to add an oxidizing agent.

The oxidizing agent can be hydrogen peroxide and / or Act potassium permanganate solution. This increases the cleaning effect in with respect to N20 and other nitrogen oxides improved as well as resinous deposits in avoided the device.

To achieve an economically favorable reaction rate it is advisable to use a raw gas that has a temperature of at least 1200 , better 1600 C and the gas to this temperature if necessary heat before it is brought into contact with the sorbent. However, it is by no means a disadvantage if the gas is at a higher temperature, because it does so can the Response can only be accelerated. So it's only then required to cool the gas before reacting if its temperature is so high is that the device used to carry out the method will be damaged could.

The process can not only be at atmospheric or reduced Pressure can be applied, but when gases are to be cleaned under increased pressure Stand pressure, the process can also be carried out under this increased pressure.

This can be used, for example, in the desulphurisation of natural gas achieve very significant economic benefits.

If calcium compounds are used as sorbents, such as for example hydrated lime and / or dolomite dust is formed during the reaction essentially calcium sulfite.

The used sorbent can then by adding air and Lime milk can be processed into calcium sulphate and this can be disposed of safely or process it into plaster. On the other hand, it is also possible to do the above used sorbent in the Claus furnace by heating the pollutants to to free. This creates calcium oxide, which is converted into hydrated lime through the addition of moisture can be implemented and reused as a sorbent.

The expelled pollutants are further processed in the Claus process, essentially forming elemental sulfur. Also the others above named sorbents can be regenerated in the Claus furnace.

A device preferred for carrying out the method has Venturi sections, which consist of pipe sections in which are in the direction of flow of the gas successively approximately centrally arranged outlet nozzles for the sorbent as well as centrally arranged approximately conical ones with their tip Displacement bodies pointing in the direction of flow and finally the pipe cross-section constricting wiper rings approximately in the shape of a conical envelope section are located. Several successive arrangements can be used in a venturi arranged by one inlet nozzle each, a displacement body and a scraper ring be.

The following are embodiments of the method according to the invention and the device used to carry it out. In the drawing Fig. 1 shows the schematic representation of a test facility.

FIG. 2 shows, as a detail from FIG. 1, a Venturi section.

Fig. 3 shows the schematic representation of a large-scale plant, 4 shows the same system in a second embodiment.

Fig. 5 shows a device for processing the calcium compounds containing sorbent.

In the in jig. 1 is the test facility to be treated at 1 Gas introduced into a R # hgasauÜneizstrecken 2. In the raw gas heating section takes place the heating of the gas to be treated to a temperature of approximately through aie open Flame of a burner that is fed with light heating oil. With the one to be treated Gas was the flue gas of a light oil-fired stove, which to Vers Also, before entering the raw gas heating section 2, it is also used with pollutants was enriched. A steam inlet opens into the raw gas heating section 2, through which water vapor can be added to the gas to be treated. On the raw gas heating section 2 is followed by a treatment section designated in its entirety by 4 a fabric filter 5 connects. The fabric filter 5 does not follow in the drawing shown, a fan, the gas to be treated through the entire device sucks and from which the treated gas escapes into the atmosphere.

In the treatment section 4, which consists of several series-connected Pipe sections 6 to 11 exist, enter, each at the beginning of a pipe section, Feed pipes 12 to 17, which are used to feed the sorbent into the reaction section serve and the outlet nozzles arranged too centrally in the pipe sections 6 to 11 18 to 23 lead through which the sorbent enters the gas stream. The sorbent is located in pressure-tight storage containers 24 to 29 from which it is taken via dosing devices 30 to 35 and via the dosing devices downstream delivery nozzles 36 to 41 with the addition of compressed air into the associated Feed lines 12 to 17 is initiated.

In each of the pipe sections 6 to 11 of the treatment section 4 follows, as can be seen in Fig. 2, on the respective nozzle lc to 23 in the by arrows designated gas flow direction an approximately conical displacement body 42 to 47. The displacement body is made up of narrow webs that the gas has no appreciable Oppose flow resistance with the inner wall of the pipe section 6 to 11 connected. These webs are not shown in the drawing. The displacement body 42 to 47 cause, as in a Venturi nozzle, a narrowing of the gases available standiiden flow cross-section.

This has the consequence that the gas flow at the end of the displacement body is placed in extremely violent turbulence, so that a very intense The added sorbent is swirled with the gas, which in turn the reaction between gas and sorbent is accelerated.

Behind each displacement body 42 to 47 is a scraper ring 48 to 53 arranged. The scraper ring is a body of about the Has the shape of a cone jacket portion or a funnel and its outer The circumference is connected to the inner wall of the pipe section 6 to 11. The scraper rings 48 to 53 act on the one hand by constricting the gas available Flow cross-section in turn as acceleration sections of a Venturi tube, on the other hand, they fulfill the task of a deposition of the sorbent on the To prevent the inner wall of the pipe, since there is no longer any sorbent deposited there would participate in the reaction and even restrict the pipe cross-section impermissibly could, rather, the sorbent is directed again and again in the middle of the pipe. Only through the scraper rings 48 to 53 is there a low pressure loss and therefore low energy consumption, such an intensive contact of the gas flow with the sorbent achieved that the extraordinarily high cleaning effect listed in the test results can be achieved.

Even if, according to common parlance, it is a Venturi route from one extending over part of the length of the route extending increasing cross-sectional reduction and a spread over a further part of the There is a subsequent cross-sectional expansion extending over the length of the route, so the term "Venturi sections" was chosen for the pipe sections 6 to 11. This was because there were two length sections in each of the pipe sections are present on which the cross-section is reduced. This is it by those length sections in which the displacement bodies 42 to 47 or the scraper rings 48 to 53 are located. Behind the displacement bodies or

With scraper rings, the pipe immediately regains its full cross-section. That part of the Venturi route within which the cross-section increases again, so is present, but its length is zero.

The reaction path 4 follows, as can again be seen in FIG. 1, a cloth filter 5 in which the sorbent is separated from the gas. That in the filter 5 accumulating sorbents can be used again in the containers 24 to 29 until its sorption capacity is exhausted or to achieve the required Cleaning effect is no longer sufficient.

The device shown in Fig. 1 can be modified by that after one or more of the pipe sections 6 to 10 additional filters or others Devices for separating the sorbent from the gas stream are arranged. This ensures that the sorbent does not have all pipe sections 6 to 11, but only one or more of these pipe sections.

Tests were carried out with the device shown in FIGS. 1 and 2 carried out. The length of the reaction section 4 was 10.35 m U to 11, from which the reaction path 4 consists, had a clear width of 310 mm. The tip of the conical displacer 42-47 was from the opening the nozzle 19 to 23 110 mm away. The length of the displacement body 42 to 47 was 140 mm, the diameter of the displacer at its circular end face was 100 mm. The distance from the end face of the displacer 42-47 up to the beginning of the wiper ring 48 to 53 was 120 mm.

The clear width of the displacement ring was 210 mm and its depth 155 mm.

During the tests, the device was used approximately every hour 9000 m flue gas piped. It arose in those not restricted by internals Divide the pipe sections 6 to 11 a gas speed of about 33 m / sec. At the At the end of the displacement body 42 to 47, the gas velocity was about 40 m / sec and at the end of the scraper rings 48 to 53 about 70 m / sec.

The flue gas from a light oil-fired furnace was used as the raw gas. The flue gas was in addition to the pollutants already present in it his entry into the raw gas heating section 2 added more sulfur dioxide.

The concentration of the pollutants contained in the raw gas, including of the added sulfur dioxide was before the entry of the raw gas into the raw gas heating section 2 determined. Furthermore, the concentration of the pollutants in question in cleaned gas behind the filter 5, not shown in the drawing measured following fan.

In the raw gas heating section 2, the raw gas was heated to a temperature heated to 1600 C. Through each of the nozzles 18 to 23 sorbent was in the Introduced gas stream, in a total amount of about 5 kg / h, accordingly about five times that stoichiometric for the complete reaction with the pollutants determined amount. Commercially available dusty hydrated lime was used as the sorbent (Calcium hydroxide, Ca (5EI) 2) used. The hydrated lime had a prior to use Moisture content of about 3 to 6%.

The sorbent was after passing through the device reused several times.

During a test operation lasting about 4 hours, the following results were found Pollutant concentrations in the raw gas or in the cleaned gas: raw gas cleaned Gas S02 2,700 mg / m3 15 mg / m H2S 1,800 mg / m3 100 mg / m N20 300 mg / m 30 mg / m This Experimental results show that with large-scale application of the invention Process calculated with a cleaning effect of at least 95% related to S02 can be.

Further experiments showed that a better utilization of the lime hyarat used as a sorbent is possible if saturated water vapor is added to the gas stream to be cleaned at 3, and indeed in such a small amount that the flowability of the dusty sorbent cannot be impaired. In addition, it was found that the cleaning effect with respect to N2 0 or Adding small amounts of hydrogen peroxide (EI202) to 3 can be significantly improved. In particular, this prevents the occurrence of resinous deposits in the system.

Further exemplary embodiments are shown on the basis of FIGS. 3 and 4.

In the large-scale plant shown in Fig. 3 takes place Supply of the gas to be treated at 101.

The gas first reaches a raw gas heating section 102 in which it if necessary, by the open flame of a heating oil burner to about 1600 C is heated. In contrast to other state-of-the-art processes, in which the gas for the purpose of cleaning to a temperature of 600 to 8000 C, but at least 4000 C must be heated, is in the process shown a higher temperature than the higher temperatures specified above should arise, can also be cleaned at higher temperatures. At 103, water vapor can be added to the gas and / or oxidizing agents, such as hydrogen peroxide, or a potassium permanganate solution be added.

The gas to be treated passes into the raw gas heating section 102 a first venturi path 104. The venturi path 104 and also all in FIGS 4 of the following Venturi sections correspond in their structure to FIG. 2, however In the example of FIG. 3 and FIG. 4, three of the in Fig. 2 shown arrangements connected in series. It is therefore for them Supply of the sorbent to the venturi section 104 three supply pipes 105, 106 and 107, which open into a common feed pipe 108, so that the Feed pipe 108 is used to feed the sorbent to the venturi section 104. A separator 109 connects to the Venturi path 104, which is used to remove the Separate sorbents from the gas. In the exemplary embodiment, it is the Separator 109 um a cyclone separator, but it can also Different types of separators for separating dust-like solids from gases are suitable to be used. It is not necessary to use the sorbent completely removed from the gas. The al, separated sorbent gets into a Leiti # iig 110.

The separator 109 is followed by three further Venturi sections 111, 115 and 119, each of which is followed by a separator 113, 117 and 121 and Finally, a last Venturi section 123, which is followed by a separator 126 is.

the separator 126 is in the exemplary embodiment a cloth filter that removes sorbents from the cleaned gas, that the respective requirements made of the cleaned gas with regard to its freedom from dust can be met.

A fan 127 connects to the separator 126, which the Forcing gas into an exhaust port or chimney 128.

The fan 127 serves to move the gas to be cleaned through the entire Suction plant. However, if the gas enters the system at a sufficiently high Pressure enters in order to be conveyed through this system by this pressure the fan 127 is not required. It should be mentioned here that the inventive The system is suitable for both gases under atmospheric or something lower Pressure cleaning is suitable as well as cleaning gases that are under a increased pressure of, for example, 40 to 60 bar.

The sorbent is in the system shown in Fig. 3 in Cycle guided. After passing through the venturi 123 in the separator 126 sorbent separated from the gas passes through a line 125, a conveying device 129 and an intermediate container 130, which can be provided with a metering device can, into the supply line 120 and from there into the penultimate Venturi section 119. The sorbent passes through in a corresponding manner the Separators 117, 113 and 109 and the Venturi sections 115, 111 and 104. From the The sorbent passes through line 110 into an adjustable separator 109 Dividing device 137, in which the amount of sorbent arriving from line 110 divided into two different partial quantities in an adjustable quantity ratio will. A minor portion is removed from the circuit through line 138. A larger subset arrives via a line 139, which in turn contains a conveying device 140 can be provided in an intermediate storage container 141, which in turn with a metering device, and from the intermediate container 141 in the supply line 124 and from there into the Venturi line 123. In addition, fresh sorbent is introduced into line 124 through line 142, and although in an amount that is eliminated through line 138 from the circuit Corresponds to the amount of sorbent. The amount to be added to the circuit at 142 fresh sorbent can due to the pollutant content of the to be cleaned Calculated and / or determined by experiments will.

The device shown in Fig. 4 differs from that Device according to FIG. 3 in that the last venturi 123 is only fresh Sorbent is passed through. The fresh sorbent gets through the pipe 143 of the Venturi line 123 is supplied. The emerging from the dividing device 137 for the return into the system a certain part is in the embodiment according to 4 via a line 144, if necessary a conveying device 145 and an intermediate container 146, which can be provided with a dosing device, is supplied via a line 147 to the penultimate Venturi section 113 and passes through then the system as in Fig. 3.

This also applies to the supply and removal of sorbent in FIG. 4 what was said above about FIG.

With the device according to FIG. 4, very small residual amounts can also be removed Remove pollutants from the gas to be cleaned. This is due to, that in the last venturi 123 only fresh sorbent is used will.

The conveying devices and intermediate containers shown in Figures 3 and 4, e.g. 129 and 130 can be omitted if the gas to be cleaned is sucked through the system. In some embodiments, the intermediate containers, e.g. 130, are omitted. As conveying devices, e.g. 129, e.g. pressure vessels or pressure transmitter can be used. These can also function as the intermediate container, e.g. 130, take over. So much for the promotion of the sorbent within the plant If a pressure medium is to be used, it can in many cases be compressed air Act. If, however, an admixture of air to the gas to be cleaned is undesirable or dangerous, as is the case, for example, when cleaning natural gas then the pressure medium can be the gas cleaned in the system or another e.g. a non-reactive gas can be used.

In the devices according to FIGS. 3 and 4 at 138 from the circuit Removed sorbents can in many cases be reprocessed. If the sorbent consisted predominantly or entirely of a calcium compound, for example from hydrated lime, and if as a pollutant, as is usually the case, predominantly If sulfur dioxide was present, it forms in the sorbent predominantly calcium sulfite. Such a sorbent can according to FIG. 5 in the Way to be worked up that it via line 138 in an oxidation tank 148, to which air is fed through a line 149. In the oxidation tank 148 there is an agent that promotes oxidation, e.g. milk of lime, so that the oxidation is carried out in the liquid phase. The milk of lime is in a container 150. The oxidation produces calcium sulfate, which in a Centrifuge 151 separated from the liquid leaving the container 148 and at 152 is derived. The liquid exiting the centrifuge 151 becomes via a line 153, optionally with the addition of milk of lime, from the container 150 via a line 15 is fed back to the oxidation tank 148.

The calcium sulphate escaping at 152 can as a result of its environmental harmlessness deposited or processed, e.g. on plaster.

The sorbent can also be worked up in such a way that that the sorbent is heated in a Claus furnace and the resulting hydrogen sulfide is processed into elemental sulfur according to the Claus process.

From the hydrated lime used as a sorbent there results after heating calcium oxide, which is converted into hydrated lime by adding moisture and can be reused as a sorbent. The last procedure described is also suitable for processing other sorbents, such as the one as well Dust-like silicon dioxide which can be used as a sorbent.

Patent claims: Blank page

Claims (28)

Claims: 1. Method for gas cleaning, in particular for Removal of pollutants from exhaust gases, flue gases and useful gases, in which the gas brought into contact with solid sorbents and separated again after sorption it is not stated that the sorbent is dusty With the pollutants reacting substances are used in such a way that they are in the Gas flow introduced ~ with this passed through venturi sections and separated from the gas will. 2. The method according to claim 1, d a d u r c h g e k e n n -z e i c h n e t that the sorbent separated from the gas is reintroduced into the gas stream will. 3. The method according to claims 1 llnd 2, d a d u r c h g e k e n It is noted that the gas flow through several successive venturi sections (104, 111, 115, 119, 123), each of which has a separator (109, 113, 117, 121, 126) is downstream, out and the sorbent first before the last of the gas flowed through Venturi section (123) and then before, against the direction of the gas flow seen, subsequent venturi sections (119, 115, 111, 4) introduced into the gas stream will. 4. The method according to claims 1 to 3, d a d u r c h g e k e n n z e i c h n e t that the circulating sorbent is a partial flow removed (138) and added a corresponding amount of fresh sorbent (142, 143) becomes. 5. The method according to claim 4, d a d u r c h g e k e n nz e i c h n e t that the withdrawal of the partial flow behind the, seen in the direction of the gas flow, first venturi (104) and the addition of fresh sorbent before, in As seen in the direction of the gas flow, the last Venturi section (123) takes place. 6. The method according to claims 4 and 5, d a d u r c h g e k e n It is not stated that only the fresh sorbent (143) is first replaced by a seen in the direction of the gas flow, last venturi (123) out and then is introduced into the sorbent cycle. 7. The method according to claims 1 to 6, d a d u r c h g e k e n It is not noted that dust-like reactive compounds are used as sorbents of alkali and / or alkaline earth metals can be used. 8. The method according to claims 1 to 7, d a d u r ch g e k e n It is not stated that hydrated lime and / or calcium carbonate are used as sorbents, especially dolomite flour> is used. 9. The method according to claims 1 to 8, d a d u r c h g e k e n It does not indicate that the sorbent is dusty turf iron ore and / or powdery Contains iron oxide, which is produced in steel production. 10. The method according to claims 1 to 9, d a d u r c h g e k e n It is not stated that amorphous silicon dioxide is dusty as a sorbent is used, which is obtained in the electrothermal production of ferrosilicon. 11. The method according to claims 1 to 10, d a d u r c h g e k e It is noted that the sorbent contains expanded perlite. 12. The method according to claims 1 to 11, d a d u r c g e k e n It should be noted that the sorbent contains dust-like filter carbon. 13. The method according to claims 1 to 12, d a d u r c h g e k e n n z e i n e t that the sorbent essentially has grain sizes below 100 #, preferably below 50 ». 14. The method according to claims 1 to 13, d a d u r c h g e k e It is noted that the sorbent contains an addition of water. 15. The method according to claims 1 to 14, d a d u r c h g e k e It is noted that the gas before contact with the sorbent is water vapor is added. 16. The method according to claims 1 to 15, d a d u r c h g e k e It is noted that the gas is oxidized prior to contact with the sorbent is added. 17. The method according to claim 16, d a d u r c h g e k e n nz e i c h n e t that the oxidizing agent is hydrogen peroxide and / or potassium permanganate solution is used. 18. The method according to claims 1 to 17, d a d u r c h g e k e It is not stated that the raw gas has a temperature of at least 1200C. 19. The method according to claims 1 to 18, d a d u r c h g e k e n n z e i c h n et that the treatment of the gas takes place under increased pressure. 20. The method according to claim 7, d a d u r c h g e k e n n -z e i c N e t that the sorbent consumed by the addition of air and milk of lime is processed into calcium sulfate. 21. The method according to claims 10 to 12, d a d u r c h g e k e It is noted that the sorbent can be removed from the Pollutants are freed and reused. 22. Device for performing the method according to the claims 1 to 21, d a d u r c h e k e n n -z e i c h n e t that the Venturi lines from Pipe sections (6 to 11) exist, in which there are in the direction of flow of the gas successively approximately centrally arranged outlet nozzles (18 to 23) for the Sorbents and centrally arranged approximately conical ones with their tips Displacement bodies (42 to 47) pointing in the direction of flow and finally the Tube cross-section narrowing approximately the shape of a conical jacket section Wiper rings (48 to 53) are located. 23. The device according to claim 22, d a d u r c h g e k e n nz e i c h n e t that there are several successive arrangements in a Venturi path of an inlet nozzle, a displacement body and a scraper ring. 24. Device according to claims 22 and 23, d a d u r c h g e k It is noted that the displacement bodies (42 to 47) on their base surfaces have about 10% of the clear pipe cross-section. 25. Device according to claims 22 to 24, d a d u r c h g e k It is noted that the clear cross-section of the scraper rings (48 to 53) is about 46% of the clear pipe cross-section. 26. Device according to claims 22 to 25, d a d u r c h g e k It is noted that removal of the tips of the displacement bodies (42 to 47) from the outlet openings of the nozzles (18 to 23 about 36% of the pipe diameter amounts to. 27. Device according to claims 22 to 26, d a d u r c h g e k It is noted that the distance between the base surfaces of the displacement body (42 to 47) and the widest points of the scraper rings (48 to 53) about 39% of the Pipe diameter is. 28. Device according to claims 22 to 27, d a d u r c h g e k It is noted that the length of the scraper rings (48 to 53) is about 50% of the Pipe diameter is.