JPS61502526A - SO↓2 and NOx separation method - Google Patents

Abstract

(57) [Summary] This bulletin contains application data before electronic filing, so abstract data is not recorded.

Description

[Detailed description of the invention] SO□ and NOx separation method The present invention is directed to the separation of SO and NOx as described in the generic concept of claim 1. The present invention relates to a method and a reactor for carrying out the method.

In this case, nitrogen oxides are converted to 1 reduced to nitrogen and water vapor under the supply of ammonia at temperatures between 00 and 170 °C. It is based on a method known per se for separating nitrogen oxides. in flue gas The S02 contained in the activated carbon/activated coke is absorbed by the activated carbon/activated coke. That and that Also, a part of S02 reacts with ammonia and turns into ammonium salt. this reaction is preferably carried out for the reduction of nitrogen oxides to nitrogen and water vapor. This suit The method helps to simultaneously separate 802 and NoX from flue gas in a special two-step process. stand on In this case, in the first step the main amount of 802 is separated, and in the second step, especially N Ox and residue -802 are separated (Richter, K.) Knoblauch, H., Tuent-g. en), German Society of Engineers (VD Engineering) - Report & 391 (1980), No. 31 2 pages).

The loaded activated carbon or loaded activated coke is sometimes treated, especially by thermal regeneration. Reactivated. In this case, 502-flue gas is produced, which is usually treated after treatment. It is converted to sulfuric acid or sulfuric acid in a process.

To reduce 5O2-emissions, so-called flue gas scrubbers have been mainly used to date. It's been coming. The flue gas scrubber is generally placed between the electrostatic precipitator and the chimney. Ru. The flue gas has a temperature of approximately 120-150°C within this range. Washing Cooling to 50-70° C. takes place depending on the process. The flue gas loses its thermal buoyancy. In order to avoid this, it is heated again, for example in a heat exchanger. Washing machine The flue gas entering the cleaner transfers heat to the flue gas coming from the scrubber, so the flue gas The gas again has a temperature of approximately 90° C. before entering the chimney.

According to the state of the art, flue gas scrubbers contain different aqueous solutions in different types of scrubbers. can be passed through. Slaked lime or limestone is the most commonly used cleaning solution. used. In the cleaning solution, sulfite is removed in solution through a chemical reaction between 802 and calcium. Calcium acid/calcium sulfate is formed and made commercially available in subsequent post-processing steps. Possible plaster can be obtained. (Kaminski (W.

'Kaminsky), 1. , -Technik) 55 (1983), pp. 673 onwards) Today, it is desired to sufficiently separate nitrogen oxides as well as S02 from waste gas. Ru. The invention therefore starts from a method of the type mentioned above, in order to separate S02. The wet cleaning method will be further improved to allow additional NOx separation. Based on the assignment.

This problem m is solved by the features of claim 1.

According to the report, it was surprisingly found that wet desulfurization and dry denitrification can be carried out in an optimal manner. 2 - Separation is currently only for a part of the flue gas, but in fact not for the majority. A small flue gas flow is diverted to bypass the washer and to the flue gas. Succeeded in mutual synchronization by utilizing the additional heating pressure of the main stream. catalytic N on activated carbon/activated coke, which therefore requires slightly higher temperatures. Ox-separation is possible under ammonia supply. S02 originating from the diversion and At the same time, the residue -8O□ still contained in the main stream is essentially absorbed. Combined with activated carbon/activated coke, according to the post-formation, the heat of activated carbon/activated coke The SO2-rich gas generated during regeneration is then subjected to wet desulfurization via a wet scrubber. It can be incorporated into commonly used post-processing processes. Therefore, in any case, dry desulfurization and desulfurization The post-treatment step to sulfuric acid or elemental sulfur required when combining nitrogen is avoided.

However, regenerating activated carbon/activated coke is another post-formation It can also be carried out in a washing machine. Thereby, the access point utilized for SO2-bonding is Recovery of ammonia and cleaning of gypsum from 5O2-washers and AK-washers Common post-treatment of liquids becomes possible.

According to the invention, existing wet scrubbers for desulphurization can be replaced at a relatively low cost. One method that can be converted into a combined desulfurization and denitrification device is shown. There is.

According to another post-formation, the loaded activated carbon/loaded activated coke is ammonium sulfate is separated and the purified suction The adhesive is fed back into the reactor for new use.

The subsequent formulation of the alternative solution is described in the civilian claims 4 to 6 of the claims. ing.

Surprisingly, the contact properties of activated carbon/activated coke are similar to those of S02 and ammonia. by partial deposition in the pore system of the reaction and the reaction products formed during it. It was also confirmed that NOx-decomposition was not affected.

Industrial implementation by screening the ammonium sulphate formed in the void volume During deposition, the pressure drop increases to such an extent that it becomes too severe in the deposit. This prevents denitrification from being interfered with. The adsorbent can be directly reused and It can be circulated and fed into the reactor. ammonium sulfate in certain cases. Some of the adsorbent may be added to the wet cleaning process if residual loading may be a problem. This still requires less equipment and energy than a full wet cleaning. This saves a considerable amount of money. The method uses direct or countercurrent, preferably horizontal It can be used in moving bed reactors with interrupted flow. sifted sulfur Ammonium acid can be post-processed into fertilizer. But it is NH3− times It can also be supplied to the public. The same is true when wet cleaning a separate stream of adsorbent; This also applies to the washing water generated during this process. Thus, the total number of substances involved in the method is Environmental integrity is guaranteed.

Another advantage is that the activated carbon/activated coke reactor is adapted to the industrial concept of claim 7. It is clear when 11# is used to implement the method according to the above. In this case, the book In the method of the invention it is necessary to separate only the residue -8o2 from the flue gas in the AK reactor. Exclusively dry process using activated carbon/activated coke and ammonia supply It is not necessary to separate all 802 as in the case of desulfurization and denitrification. The circumstances will be taken into consideration.

The invention will now be described in detail with reference to the drawings and examples.

Figure 1 shows the combined desulfurization and denitrification with activated carbon/activated coke thermal regeneration. A schematic diagram of the process of extraction is shown, Figure 2 shows the combined desulfurization with activated carbon/activated coke regeneration in wet cleaning. - and a schematic diagram of the denitrification treatment process, Figure 3 shows the combination when introducing loaded activated carbon/loaded activated coke onto a sieve. A schematic diagram of the process of desulfurization and denitrification is shown, Figure 4 shows the method according to Figure 3 when supplying a separated stream of cleaned adsorbent to a wet washer. shows a schematic diagram of other formations of working methods; FIG. 5 shows an AK-reactor which is particularly suitable for residue-8*2-separation.

As is clear from FIGS. 1 and 2, 502- and NOx- coming from furnace 1 The entire stream of flue gases 20 desulfurizes the flue gases before entering the wet scrubber 10 For this purpose, the flue gas main stream 2 and the flue gas branch 9 I/l are distributed. Flue gas - main Stream 2 is conducted via heat exchanger 11 into wet scrubber 10 . small amount of flue gas The split stream 9 bypasses the heat exchanger 11 and the wet washer 10 and directly supplies activated coke/ Flows into activated carbon-reactor 12 (AK-reactor). First, the flue gas branch 9 is Cooled and fully depleted of 802 and partially KNox - flue gas - main stream 2 and the flue gas main stream is mixed after being reheated in the heat exchanger 11. . Mixed flue gas - branch 9 and flue gas - main stream 2 and then recombined flue gas - total The temperature of the body stream 7 is below the temperature of the overall flue gas stream 20 coming from the furnace 1, but In the reactor 12 there is no possibility of catalytic NoX reduction with activated carbon or activated coke. That's enough. However, the recombined flue gas-total stream 7 has a fully desulphurized flue gas The gas has a higher 5o2 content than the main stream 2. By the way, surprisingly, this This slightly higher 502 - It is clear from the content that there are no defects at all, except for the slightly higher amount of ammonia used. I made it clear. Furthermore, only the reduced flue gas flow flows through the wet scrubber 10 and the damp At the same time in the washer, the cleaning capacity remains unconstrained and can be further expanded elsewhere as described below. It is preferable that it can be used in

AK-reactor 12 is equipped with N after adding ammonia into the combined flue gas stream 7. Used to remove Ox and 802 at the same time. AK - Clean leaving reactor 12 The reduced flue gas stream 8 is combined with the combined total flue gas stream 7 before the AK-reactor 12. It also has a slightly higher temperature.

and the NOx reduction depends on the NH3 addition and the design of the AK reactor 12. It can range from 20 to 90 inches.

The activated carbon/activated coke in the AK-reactor 12 is gradually converted into ammonium bisulfate and and ammonium sulfate, thus at least in part over the time interval. It must be removed or regenerated in succession (・.

According to FIG. 1, this is carried out thermally in the AK regenerator 13. Second activated coke or activated carbon can be prepared by contacting it with hot sand in a known manner. by circulating heat-rich gases or by combustion waste gases. heated. The SO2-rich gas obtained in this way does not meet the current state of the art. Accordingly, it can be further processed into sulfuric acid or elemental sulfur in a separate unit. and By the way, a special advantage of the proposed method is that it is possible to The soldering gas stream 14 is simultaneously sent to the flowing flue gas main stream 2 via the wet washer 10. It's about being able to do something. The SO2 from the regenerator (S02-rich gas stream 14) is The flue gas is separated together with S02 from the main stream 2 in the washer 10. That's it Thus, the volumetric flow of flue gas increases slightly. Of course, the 502 concentration is between 10 and 40 only increased. The main stream 20 flowing through the wet washer 10 has a reduced amount of flue gas. Therefore, sufficient capacity is required to separate this additional 5O2- amount and thus allow for conventional post-treatment. It can be used to incorporate it into the post-treatment of plaster, for example.

In addition, according to FIG. Therefore, it can be done. Activated coke/activated carbon in AK-reactor 12 The water must be separated in a separate AK-dryer 31 before reuse. AK-washing The cleaning liquid from the vessel 30 contains ammonium sulfate as well as ammonium hydrogen sulfate and Also contains sulfuric acid.

The ammonium sulfate from the cleaning solution is removed by additionally supplying ammonia. Been formed. However, ammonium sulfate solution is concentrated by evaporation to solid ammonium sulfate. Post-processing by shrinking is known to be extremely expensive. child The disadvantage of this concept is that the liquid leaving the AK washer 30 contains Ca in the Ca precipitator 32. avoided by adding (OH)2 or CaCO3 (in this case this These two materials are also used to remove S02 in flue gas cleaning molds).

By adding Ca-compound, ammonium sulfate is converted to calcium sulfate ( gypsum), in which case ammonia is liberated and removed from the liquid again by pipping and added to the flue gas before the AK-reactor 12. supplied again. Therefore, anyway, catalytic NOx-reduction and residual-802-binding If so, NH3 must be added and therefore NH3 must be recycled The use of fresh NH3 is thus avoided. Ca - Ca-containing from the precipitation separator In common with the wastewater generated from the flue gas washer, the wastewater is treated especially in the final stage in the aftertreatment device 33. The product is post-processed into plaster. Therefore, the sulfur from the activated coke/charcoal regenerator is A separate work-up of the yellow compound is avoided.

As a result, the existing flue gas scrubber 10 can be used in a particularly advantageous manner with activated carbon/activated co-carbon This can be assisted by catalytic NOx reduction at the combined 5O2 - Removal and NOx removal The apparatus illustrated in FIGS. 1 and 2 is used exclusively. When compared with conventional flue gas scrubbers used for flue gas desulfurization, the It turns out that synergistic effects can be achieved through new technical ideas by combining This is because in the AK reactor 12 additionally the remaining residue of the flue gas 802 Since 5O2- is separated most thoroughly, good 5O2- separation is also achieved along with NO air removal. Because it will be achieved.

502 - Flue gas scrubbers present for the removal of activated coke or activated carbon No additional cost required for after-treatment of the 5O2vc-rich gas generated during regeneration. The illustrated method for NOx removal can be prepared later without the need for Wear.

As is clear from FIG. and introduced into the AK-reactor 12. The flue supplies ammonia to the gas stream via conduit 46. is added. It is possible to simultaneously separate NOx and 802 in the AK-reactor 12. be called. The cleaned flue gas stream 45 leaving the AK-reactor 2 is partially S O2 is separated. NOx-reduction depends on ammonia addition amount and AK-reactor Depending on the design of 12, it can range from 20 to 90 inches.

The activated carbon/activated coke in the AK-reactor 12 is gradually converted into ammonium bisulfate and and ammonium sulfate. The adsorbent is guided in continuous circulation and this If ammonium sulfate is separated from the adsorbent by rs43, and the adsorbent is It is fed back into the moving bed reactor in conduit 44 for further use. sifted sulfur Ammonium acid can be supplied for appropriate use.

According to Fig. 4, reference numbers 41 to 46 are the same as in the case of the working method described in Fig. 3. have meaning. Moreover, according to FIG. 4, the screened adsorbent stream 50 is Regenerated in the washer. This regeneration is carried out by washing away with water in the AK-washer 47. It is done by.

The activated coke/activated carbon is reused in the AK-reactor 12 in a separate AK-drying unit. The water must be separated at stage 48. The cleaning liquid from the AK-cleaner 47 is It also contains sulfur.

In the case of this variant of the solution as well, the liquid leaving the AK-cleaner 47 via the conduit 51 contains - Ca(oH)2 or CaCO3 is added in the precipitation separator 49; Also, Screened ammonium sulfate can be introduced into the liquid via the conduit 52. Wear. Calcium sulfate is converted from ammonium sulfate by adding C4-compounds. This causes the formation of gypsum, in which case ammonia is liberated, The flue gas 4 (AK-reactor 12 via conduit 53. Therefore, contact NOx- NH3 must be added for reduction and 5O2-bonding, therefore NH3 By recycling the NH3, the use of fresh NH3 is avoided. Ca-precipitation separation The Ca-containing wastewater from the device is connected by conduit 54 to the wastewater originating from the flue gas washer. Commonly, in the after-treatment device 55, in particular the finished product, plaster, is after-treated. Therefore, the active covalent Separate post-treatment of sulfur compounds from carbon/activated carbon regeneration units is avoided. Ru.

Design example 1 The table below and Figure 1 show the flue gas cleaning equipment based on new technological ideas. Design examples are included.

The example is a constant flue gas volumetric flow, in this case ioo,oo.

m3A (in standard conditions) with a given 802-content, in this case So□'2000 m y/rn3 (in standard conditions) and a given nod Ox-content, in this case NO2120 0”97m3 (under standard conditions), (the ratio of N02 to NOx is approximately 8 m3) ) and a temperature of 130°C. Flue gas - Main stream 2 is 75.00 0 m”A (standard state) volumetric flow and accordingly lead into the bypass path. The flue gas flow 9 is 25,000 m”A (standard condition). After the exchanger 11 and before the wet scrubber 10 the temperature is 85°C and the flue gas scrubbing At the end of the vessel it is 65°C. By reheating in the heat exchanger 11, the temperature is reduced to 1 01°OK will be raised. After refeeding the flue gas branch 9, the temperature is further increased to 108°C. A temperature increase is obtained, which is sufficient for catalytic No air removal. AK- A temperature increase to 109° C. takes place again in reactor 12, so that the temperature in the chimney increases. Sufficient buoyancy of the cleaned flue gas 8 is ensured.

The 5O2 content in the wet washer 10 ranges from 5o22000 my/mis to 200 m9/m3 (at standard conditions), NOx-content is reduced to No21200I n9/z” to 11431 m3 (in standard conditions). The recycled S02-rich gas stream 14 is transferred from the AK-regenerator a13 to the flue gas-main stream. 2, the flue gas volumetric flow in the wet washer 10 is 75.0 00 m3A to 76,000 m3/h (in standard conditions).

After the flue combines the sous branch stream 9 with the flue gas main stream 2, the combined flue gas overall temperature 7 The 5O2- content in is again S0265 [] mli’/m3 (m quasi-state Te) NOx-content increases from NO21140rrui/m” to 1154rrui/m” increases to rQ/m3 (at standard conditions). Before the AK-reactor 12, the NH3- addition is , the NH3- content in the flue gas of NH3608m9/-3 (standard state Te) is obtained. It is done in the amount that can be done.

Furthermore, 502 to 50260iy/m3 (at standard conditions) in the AK-reactor 12 - a decrease in content occurs and NO to No2200m9/rn3 (in standard conditions) A decrease in the x-content occurs. These two values are essentially 5024 from now on 00 m9/m3 (in standard conditions) or NOx 200 mg/m3 (in standard conditions) If the flue gas is below the value that you should strive to obtain (in the

Design example 2 Example 2 is based on the same operating conditions (table below).

According to figure 2, reference symbols have the same meaning as in the case of the working method described in figure 1. has.

After converging the flue gas branch 9 with the flue gas main stream 2, the combined flue gas overall temperature 7 The 802- content in it increases again to 650 mg/m3 (at standard conditions) of So2, The NOx content varies from N021140In9/m" to 115411/m" (standard (in a quasi-state). AX-5, NH3- addition in front of generator 12 is NH36 08"9/" (standard condition) be called.

Furthermore, 802 to 802601n9/m3 (at standard conditions) in AK-reactor 12 - a decrease in the content and NOx to NO2200 m9/m3 (at standard conditions); - a decrease in content occurs; These two values are essentially 50240 from now on 0m9/m3 (in standard conditions) or NOx2001m3 (in standard conditions) flue It's below what you should be trying to get gas from.

The cleaning liquid for the wet washer 30 for AK-regeneration is 0.13 mol/l. Water with an NH4 content of 7.65 yx3/h fif is required (!: Sarel .

Design example 3 The flue gas from the coal furnace is treated with a charcoal calcium aqueous solution (cleaning after post-treatment of the cleaning liquid). The flue gas scrubber with the final product (from the gypsum) is removed (after reheating) under Ru; Flue gas volumetric flow: 100.000 m3//h (under standard conditions) Temperature: 900 C Morozine content: 6.2 liters Sulfur dioxide content fi: 5o2400η/m3 (in standard conditions) Nitrogen oxide content @ : NO2800m9/m3 (standard condition) (N025% to NOx) Add NH337, 0 kg/h to the flue gas to a layer depth of 2. Clmt: 3 and 155m It is added before a moving bed reactor with a cross-sectional area (flow area) of 2. The moving bed reaction The vessel is filled with activated carbon, which in the supplied state has a voltage of 580 kV 1713 The bulk density of Solnauer, Emlett and Teller (Brunauer) A specific surface area of 450 m2/9 according to Emmett und Teller) (DIN66131). 4.7 m3 of activated coke per hour is placed under the reactor. Remove from the end and sieve to remove dust and sulfur adhering to the outer surface. ammonium acid is separated) and fed back into the top of the reactor. During sieving , 53.6 kg/h of ammonium sulfate is produced.

The cleaned flue gas is converted to nitrogen acetate after the reactor, calculated as NO2. 2190 m9/-” (in a quasi-state) (NO, X vs. NO2O ratio less than 1%) (full) and 5o2140/-3 (IF (in quasi-state)).

Design example 4 (Comparative example for design example 6) The flue gas leaves the flue gas washer under the same conditions as in Design Example 6. moving bed reaction The vessel has a flow area of 1557 x 2 and a bed of 2.0 m as in Design Example 3. It has depth. The moving bed reactor is charged with regenerated activated coke from above, The activated coke has a bulk density of 580 kg/m' and a Solnauer , Brunauer, Kmmett and Te 1ler) with a specific surface area of 450 m2/jj (D-work N66131). do. The flue gas is fed with 342.3 kg/h of NH before the moving bed reactor. every At the time, 3.4 m3 of activated coke was taken out from the bottom of the reactor and regenerated again. Move to. The flue gas leaving this reactor is No. 2190~/rn3 (under standard conditions) (NO2O ratio to NOx less than 1-) and 5o240 m9/”3 (standard in a quasi-state).

, the design example further improves the ability to circulate activated coke without expensive regeneration (Design Example 3). The amount of NH3- to be supplied to the In this case, the NOx separation is equally good. For design example 4 In practice, a more favorable 5O2-value is achieved, but the 502-separation in design example B is , still much lower than the value required by the legislator.

Particularly preferred is the introduction of activated carbon/activated Fuchs into the AK-reactor 12 in the fifth stage. This is the case when it is done by drawing. Corresponding to the current state of the art, transverse flow is carried out. In the case of a moving bed reactor, the particulate adsorbent/catalyst material is fed from a single point at the head of the device; and removed from one part of the leg for regeneration. Conical introduction-and-exit armor Flows uniformly through the unique adsorption/reaction space confined by the door. The flow rate is If the flue gas to be cleaned contains dust (blockage due to dust accumulation) or if the flue gas is The solid component (e.g. 802 in this case) is separated so that it is adsorbed (reduction in adsorption capacity). (low), the speed must not be reduced below a certain minimum speed. In both of these cases, adsorption/ The rear part of the reaction volume in the direction of gas flow has a small load there. Not used enough. The solution is already to operate the two steps in separate adsorption equipment. is proposed, in which case the removal of the slightly loaded granular adsorbent from the adsorption device in cylinder 2 The removal rate is lower than the removal rate from the first adsorption device. Two separate adsorption devices According to the invention, the cost of the separation member is gas permeable but particle impermeable. This can be avoided in the case of the operation method illustrated in Figure 5 when 15 is installed. Wear. The separating element 15 extends into the upper conical part 16 of the AK-reactor 12. that leads downwards to a separate removal unit 17,18 for granular material.

Through the removal unit the granular material undergoes different loads in the two layers 19 and 21. It is taken out at different speeds for equilibration.

Furthermore, the volume of the space through which the flow flows can be distributed in different ways via the separating member 15. 19.21, whereby another method of balancing different loads in the two layers 19.21 determined. As separating element 15 a special grid can be used or Uniform AK-discharge in the reactor leg without separation elements 15 using perforated plates For an AK-reactor 12 with a volume of 270 when the layer depth is 1.75 m An AK-reaction capacity of m3 is obtained. AK-31 to be derived for regeneration is as follows: 6. It would be 8m3/h.

Separate AK- from the separation member 15 and the two layers 19.21 under comparable conditions When using an AK-reactor 12 according to the invention with a discharge unit 17.18 If the depth of the total layer is 1.75 m, the following values are obtained: The depth of the layer is 0.77 m, and the depth of the layer on the gas outlet side is 0.98 m. This further corresponds to the AK-full capacity of 270 F113.

1 on the gas inlet side due to the expected different evacuation rates from the two layers 19.21. ．． 357X3/h and 0.95 m'/h are discharged on the gas outlet side, and this corresponds to a total mold pressure of AK3.3 m3/h to be derived for regeneration.

From this, it follows that the AK-fi to be regenerated every hour is 0.5 fi than in the comparative example using a reactor according to the state of the art. It turns out that it is lower by 3/h.

Design examples corresponding to Figures 1 and 2 Wan District 1 Figure 2 Figure 4 Figure 5 international search report ANNEX To’hrm INTERNATIONAL SEA CHRE PORτ ON Spring 1 page continuation Priority claim [Phase] 198 Group June 28 [Phase] West Germany (DE) [Yes] P34 23761, 5 ■ 198 Bo "August 16 [phase] West Germany (DE) ■ P34299 Founded on 99.8 by Knoblauch, Karl, Federal Republic of Germany Author Richter, Etzkenord Federal Republic of Germany @ Author Grochofs Key, Horst, Federal Republic of Germany - SE (no address) 4300 Essen, Semperstrasse 554300 Erasen 18. Schmachtenbergsch 4200 Oberhausen, Halfenstra

Claims (8)

[Claims] 1. S02 and NOX are separated in particular from the flue gas, in which case the SO2 is removed in the first step. 2 and a minor amount of NOx are separated from the flue gas and removed from the flue gas in a second step. The main amount of NOx from the gas is removed with activated carbon/activated coke in the reactor under ammonia supply. in a method in which the residue -S02 is separated by reaction with ammonia. a) distributing the entire flue gas flow from the furnace into a flue gas main stream and a flue gas branch stream; b) Flue gas - main amount of S02 and minor amount of NOX from the main stream in a wet scrubber and subsequently reheating the main flue gas, c) the flue gas - the flue gas whose main flow is guided past the wet washer in a bypass path; - A method for separating SO2 and NOX, characterized by splitting and concentrating. 2. Activated carbon/activated coke is thermally regenerated to generate SO2-rich gas and S 02-enriched gas stream and the flue gas main stream in front of the wet washer. The method described in Scope 1. 3. Activated carbon/activated coke connected activated carbon/activated coke - dryer and reactor Activated carbon/activated coke into the reactor - regenerated in a wet washer with recirculation path, A K-addition of Ca(OH)2- or CaC03- to the cleaning solution of the washer (Ca-precipitate ammonia recirculation and S02-cleaner and According to claim 1, the cleaning liquid from the and AK-cleaners is commonly post-treated to plaster. the method of. 4. The activated carbon to be loaded and the activated coke to be loaded are led from the reactor through a sieve and then to separate ammonium sulfate and use the purified adsorbent again. 2. The method of claim 1, wherein the reactor is re-fed. 5. A substream of the cleaned adsorbent is fed into a wet washer, followed by drying, and 5. The method of claim 4, wherein the reactor is fed back. 6. The sieved ammonium sulfate is made into a solution, the ammonia is expelled, and the treated 5. The method of claim 4, wherein the method is recirculated as much as possible. 7. Extracts ammonia from ammonium sulfate in wash water and recirculates it into the treatment process. 6. The method according to claim 5. 8. For carrying out the method according to any one of claims 1 to 7. In the second activated carbon/activated coke reactor, the reactor (12) is gas permeable. It has a separation member (15), which separates the reactor (12) into two spaces (19/2). 1), and the space has a separate outlet for activated carbon/activated coke (17/18) Activated carbon/activated coke reactor, characterized in that it has: