RU2746006C1 - Method of waste recycling - Google Patents

Abstract

FIELD: environmental protection.

SUBSTANCE: invention relates to the field of environmental protection. It can be used in the recycling of waste from industrial facilities in chemical, agricultural, food and other industries. The initial waste is incinerated in the presence of a mixture of air and a reducing agent – aqueous solutions of carbamide or ammonia. The mixture is sent to the drum-type furnace for combustion at a linear speed of 6 to 25 m/s in two directions - along the flue gases in a turbulent mode and perpendicular to their direction from top to bottom. The combustion product, consisting of slags and flue gases, is subjected to afterburning at a temperature of 1300-1500ºC, for no more than 2 seconds with simultaneous recovery with a heat transfer coefficient of 30-60 W/m2K. At the same time, ash and slag waste and the first flue gas flow are obtained. This stream is sent to the scrubber for cleaning by interacting for no more than 2 seconds initially with a calcium-containing alkaline reagent in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension, and then at a temperature of 180-200ºC with a gas purification catalyst. The resulting second flue gas stream is subjected to cyclone cleaning with the formation of cyclone cleaning waste and a third flue gas stream. This stream is fed to the mixing stage with a powdered sorbent to produce a fourth flue gas stream, which is sent to the bag filter for cleaning. The resulting purified flue gases are dumped into the atmosphere, and the waste generated during cleaning is recycled to the mixing stage with a powdered sorbent.

EFFECT: a high degree of contact of initial waste, air and reducing agent in the drum-type furnace, and flue gases with sorbents when cleaning these gases from pollutants.

3 cl, 3 ex, 2 tbl

Description

The invention relates to the field of environmental protection and can be used in the processing of industrial waste of chemical, agricultural, food and other industries.

Currently, the presence of a significant amount of various wastes and their treatment are a serious environmental problem.

There is a known method of high-thermal neutralization of liquid, pasty, their mixtures and solid waste, including loading and incineration of waste, afterburning of gaseous products when supplying air activated by a corona discharge and emission of waste gases, in which, after afterburning, gases are quenched with subsequent absorption (RU 2614999, 2018 ).

In this case, air activation by a corona discharge at the afterburning stage is carried out with a mode of 350-450 discharges per second at an electric field strength of up to 8 kV / cm and additionally supplying air activated by a corona discharge is carried out when loading waste with a mode of exposure to a corona discharge of 500-650 discharges per second at an electric field strength of up to 11 kV / cm, during quenching with a corona discharge mode of 350-450 discharges per second at an electric field strength of up to 8 kV / cm, during absorption with a corona exposure mode, a discharge of 350-450 discharges per second at an intensity electric field up to 8 kV / cm, when exhaust gases are emitted with a corona discharge mode of 250-350 discharges per second at an electric field strength of up to 6 kV / cm. The disadvantages of this method are the use of a complex technological scheme and high energy consumption.

Closer to the invention is a method of incineration of municipal solid waste and other organic waste and a device for its implementation (RU 2249766, 2005).

The known method includes incineration of waste by supplying pre-heated air, afterburning of gaseous combustion products, subsequent treatment for binding HCl, Cl ₂ , HF, passing through a heat exchanger-boiler, gas cleaning. At the same time, before being fed into the furnace for incineration, the waste is separated, the organic part of the waste is crushed to a size of no more than 100 mm, the waste is mixed with air heated to a temperature of 300-400 ° C, the feed into the cyclone furnace is carried out tangentially with a linear speed of at least 28 m / s ... Combustion is carried out at temperatures of 1320-1350 ° C, afterburning is carried out in a catalytic afterburner at temperatures of 1300-1500 ° C, treatment for binding HCl, Cl ₂ , HF is carried out in a limestone decarbonization chamber to obtain quicklime. Before being fed to the boiler, the processed combustion products are passed through an air heater, and after the boiler - through a wet gas cleaning system, and the boiler's thermal energy is supplied to consumers.

The disadvantages of this method consist in the need for additional costs for grinding waste, heating air to a high temperature, and using catalysts at the high-temperature stage of afterburning. At the same time, at temperatures of 1320-1350 ° C and a linear speed of air flows of at least 28 m / s, a rapid depletion of the furnace walls occurs in the cyclone furnace, which leads to high operating costs. The quicklime CaO obtained by the above method will have a high content of heavy metals in its composition, which significantly reduces the range of its application in industry. Based on the description of the known method, the degree of flue gas cleaning does not exceed 75%. Thus, the known method is not effective enough.

The technical problem to be solved by the present invention is to increase the efficiency of the processing method and the degree of purification of flue gases.

The specified problem is achieved by the described waste processing method, which consists in the fact that the original waste is incinerated in a drum furnace at a temperature of 900-1000 ° C in the presence of a mixture of air and a reducing agent - aqueous solutions of urea or ammonia, which is sent for incineration into a drum furnace at a linear speed from 6 to 25 m / s in two directions - along the course of flue gases in a turbulent mode and perpendicular to their direction from top to bottom, the product formed during combustion, consisting of slags and flue gases, is subjected to afterburning at a temperature of 1300-1500 ° C, no more than 2 sec with simultaneous recuperation with a heat transfer coefficient of 30-60 W / m ² K with the production of ash and slag waste and the first stream of flue gases, which is sent to the scrubber for cleaning by interaction for no more than 2 sec initially with a calcium-containing alkaline reagent in the form of an aqueous suspension and sorbent in the form of an aqueous suspension, and then at a temperature of 180-200 ° C with a purification catalyst g the resulting second stream of flue gases is subjected to cyclonic cleaning with the formation of cyclonic waste and a third stream of flue gases, which is fed to the stage of mixing with a powdered sorbent to obtain a fourth stream of flue gases, which is sent to a bag filter for cleaning, the resulting cleaned flue gases discharged into the atmosphere, and the waste generated during cleaning is recycled to the stage of mixing with a powdery sorbent.

In this case, lime, dolomite flour, limestone flour are used as a calcium-containing alkaline reagent in the form of an aqueous suspension; shale ash, zeolite, activated carbon, activated alumina, silica gel, activated alumina or a mixture thereof are used as a sorbent in the form of an aqueous suspension, and As a powdered sorbent, quicklime, slaked lime, limestone, shale ash, zeolite, dolomite, activated carbon, activated alumina, silica gel, iron (II) hydroxide, magnesium oxide, zinc oxide, cobalt oxide, calcium oxide, iron (III) chloride are used , copper oxide, copper sulfate, copper phosphate, lead sulfate, lead phosphate, cadmium sulfate, cadmium phosphate, activated alumina, or a mixture thereof.

The achieved technical result is to provide a high degree of contact of both the original waste, air and reducing agent in the drum furnace, and flue gases with sorbents when cleaning these gases from pollutants.

The essence of the invention is as follows.

It is known that incineration of waste produces flue gases containing, in particular, underburned products, in particular CO, C ₂₀ H _12. , Nitrogen compounds: NO _x (NO + NO ₂ ,), HNO ₂ , HNO ₃ , NH ₃ , HCN, phosphorus compounds: P ₄ O ₁₀ , P ₂ O ₅ (above 1100 ° C), H ₃ PO ₄ , sulfur compounds: SO ₂ , SO ₃ , H ₂ S, H ₂ SO ₃ , H ₂ SO ₄ , compounds chlorine: HCl, Cl ₂ , fluorine compounds: HF, polychlorinated dibenzo-n-dioxins (PCDD) and polychlorinated dibenzofurans (PCDF), heavy metals, in particular mercury (Hg), lead (Pb), cadmium (Cd), thallium ( Tl), antimony (Sb), arsenic (As), lead (Pb), chromium (Cr), cobalt (Co), copper (Cu), manganese (Mn), nickel (Ni), vanadium (V).

When carrying out the described method, it is possible to use various types of production and consumption waste (solid, liquid and pasty), in particular, such as, inter alia, medical waste of classes A, B, C, D, oily waste, household waste.

In this case, solid waste is loaded into the receiving hopper using a belt conveyor. Pasty and liquid waste is sent to the receiving hopper separately, using a screw conveyor.

From the receiving hopper, the waste is directed by a pusher into the rotary drum kiln. Burners are used to ignite the waste and maintain the required temperature. In this case, it is possible to use various types of fuel, for example, diesel fuel in accordance with GOST 305 / GOST R 52368, natural gas in accordance with GOST 5542, liquefied gas in accordance with GOST 20448, GOST 27578, GOST 21443, motor fuel GOST 1667, fuel oil GOST 10585, oil GOST 10585 , oil 51858, GOST 9965.

The original waste is incinerated at a temperature of 900-1000 ° C in the presence of a mixture of air and a reducing agent - aqueous solutions of urea (urea content 20-40%) or ammonia (ammonia content 5-10%). This neutralizes, in particular, nitrogen compounds NO _x (NO + NO ₂ ,), HNO ₂ , HNO ₃ , NH ₃ , HCN. Urea consumption is 2-8 g / kg waste, ammonia consumption is 1-10 g / kg waste.

A mixture of air and a reducing agent - aqueous solutions of urea or ammonia is directed into a rotary kiln at a linear speed of 6 to 25 m / s in two directions - along the course of flue gases in a turbulent mode and perpendicular to their direction from top to bottom.

The specified mixture is fed through the feed channels, which are made in the upper part of the furnace. In this case, a mixture of air and reducing agent, directed into the furnace along the flue gases, is fed through channels with turbulators installed inside them.

As a result, multidirectional, including turbulent, mixing of the processed waste and a mixture of air with a reducing agent is provided in a rotary drum furnace, leading to an increase in the degree of contact of the mixed components.

The product formed as a result of combustion, consisting of slags and flue gases, is subjected to afterburning in an afterburner at a temperature of 1300-1500 ° C, for a time not exceeding 2 seconds with simultaneous recuperation at a heat transfer coefficient of 30-60 W / m ² K to obtain the removed ash and slag waste and the first flue gas stream.

The afterburner also undergoes thermal destruction of polychlorinated dibenzo-n-dioxins (PCDD) and polychlorinated dibenzofurans (PCDF).

The afterburner is equipped with a recuperator. The used recuperator is designed to remove excess heat from flue gases and stabilize the temperature processes of combustion in the afterburner and drum furnace. A heat carrier, in particular water, is supplied inside the recuperator, and heat exchange is carried out between the heat carrier and flue gases through a separating heat transfer surface. The heated coolant is sent to consumers.

At the same time, with a heat transfer coefficient above 60 W / m ² K, the efficiency of heat transfer decreases, which leads to inefficiency of combustion processes. With a heat transfer coefficient below 30 W / m ² K, the recuperator elements are clogged with soot and lumps are formed, which disrupts gas exchange and leads to partial or complete failure of the afterburner.

The first stream of flue gases is directed to the scrubber for cleaning by interaction for no more than 2 seconds. initially with a calcium-containing alkaline reagent in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension, and then at a temperature of 180-200 ° C with a gas purification catalyst.

A calcium-containing alkaline reagent in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension are fed into the upper part of the scrubber through nozzles installed in its upper part.

In this case, shale ash, zeolite, activated carbon, activated alumina, silica gel, activated alumina or a mixture thereof are used as a sorbent in the form of an aqueous suspension.

As a gas purification catalyst, it is possible to use, in particular, such as FCR-71, FCR-91, Filtra DS-90E, Cu / ZSM-5, Cu / SAPO-34.

In the scrubber, flue gases are purified from a wide range of pollutants, in particular, such as underburned products (CO, Ca ₂₀ H ₁₂ ), phosphorus compounds (P ₄ O ₁₀ , P ₂ O ₅ , H ₃ PO ₄ ), nitrogen compounds (NO _x (NO + NO ₂ ,) and others, sulfur compounds (SO ₂ , SO ₃ , H ₂ S, H ₂ SO ₃ ), heavy metals: Cu, Zn, Hg, Cd, Pb, Sn, Fe, Mn , Ag, Cr, Co, Ni, As, Al, Ga, Ge, Mo, Sb, Te, W, Tl, Bi.

In this case, due to the evaporation of water contained in aqueous suspensions, the reaction products are in the form of dry dust (fly ash).

The resulting second flue gas stream is subjected to cyclonic cleaning with the formation of cyclonic waste and a third flue gas stream. Cyclonic cleaning is carried out at a temperature of 180-200 ° C for no more than 2 seconds. Cyclonic waste is a fly ash with a particle size of 5-25 microns.

The third flue gas stream is fed to the stage of mixing with a powdered sorbent to obtain waste and a fourth flue gas stream. The contacting process at the mixing stage is carried out at a temperature of 180-200 ° C. The mixing step can be carried out, for example, in a mixer.

As a powdered sorbent, quicklime, slaked lime, limestone, shale ash, zeolite, dolomite, activated carbon, activated alumina, silica gel, iron (II) hydroxide, magnesium oxide, zinc oxide, cobalt oxide, calcium oxide, iron chloride (III ), copper oxide, copper sulfate, copper phosphate, lead sulfate, lead phosphate, cadmium sulfate, cadmium phosphate, activated alumina, or a mixture thereof.

In this case, additional neutralization of such pollutants as, in particular, phosphorus compounds (P ₄ O ₁₀ , P ₂ O ₅ , H ₃ PO ₄ ), sulfur compounds (SO ₂ , SO ₃ , H ₂ S, H ₂ SO ₃ ), chlorine compounds (HCl, Cl ₂ ,) fluorine compounds: HF, heavy metals: Hg, Pb, Cd, Tl, as well as PCDD, PCDF.

The resulting fourth stream is directed to a bag filter for cleaning. Cleaning is carried out at a temperature of 180-200 ° C.

The obtained purified flue gases are discharged into the atmosphere, and the waste generated during the cleaning, which consists of both spent and partially spent powdery sorbents, is recycled to the stage of mixing with a powdery sorbent. The choice of the type of calcium-containing alkaline reagent in the form of an aqueous suspension, sorbents in the form of an aqueous suspension, powdered sorbents and their amounts depends on the type of initial waste.

Example 1.

A mixture of medical waste of classes A, B, C, D (class A - 10%, class B - 40%, class C - 25%, class D - 25%) is incinerated in the presence of a mixture of air and a reducing agent - an aqueous solution of urea.

A mixture of air and reducing agent is directed for combustion into a rotary drum furnace with a linear speed of 6 m / s in two directions - along the course of flue gases in a turbulent mode and perpendicular to their direction from top to bottom.

The specified mixture is fed through the feed channels, which are made in the upper part of the furnace. In this case, a mixture of air and reducing agent, directed into the furnace along the flue gases, is fed through channels with turbulators installed inside them.

The combustion is carried out at a temperature of 900 ° C. The urea content in the solution is 30%. Urea consumption is 7.5 g / kg waste.

The product formed as a result of combustion, consisting of slags and flue gases, is subjected to afterburning in an afterburner at a temperature of 1300 ° C, for a time not exceeding 2 seconds, with simultaneous recuperation to obtain removed ash and slag waste and the first stream of flue gases.

Water is supplied to the recuperator installed in the afterburner and heat exchange is carried out between the coolant and flue gases through the separating heat transfer surface. The heat transfer coefficient is 30 W / m ² K. The heated heat carrier is sent to consumers.

The first stream of flue gases is directed to a scrubber, where it is reacted for no more than 2 seconds, initially with slaked lime in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension - NaA zeolite with a mass ratio of water: lime: NaA zeolite equal to 1.0: 0 , 20: 0.7 (the total amount of water contained in aqueous suspensions of lime and sorbent is taken into account), and then at a temperature of 180 ° C with a gas purification catalyst located in the lower part of the scrubber.

Lime in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension are fed into the scrubber through nozzles installed in its upper part.

An alumina-based FCR-71 gas purification catalyst is used as a catalyst.

The second flue gas stream formed after passing through the scrubber is subjected to cyclonic cleaning for less than 2 seconds at a temperature of 180 ° C with the formation of cyclonic cleaning waste (fly ash) and a third flue gas stream.

The specified third stream of flue gases is directed to the mixing stage, where it is subjected to contact in a mixer with a powdered sorbent. As a powdered sorbent, a mixture of powdered lime, activated carbon and iron (II) hydroxide is used with a mass ratio of powdered lime: activated carbon: iron (II) hydroxide equal to 1.0: 0.35: 0.11.

This produces a fourth flue gas stream and waste. The fourth stream of flue gases is directed for cleaning into a bag filter at a temperature of 180 ° C.

The flue gases purified in the bag filter are discharged into the atmosphere, and the waste generated during purification is recycled to the mixing stage, to the mixer.

Example 2.

Oil-contaminated drill cuttings with a content of oil products in the amount of 20% by weight are used as waste. The specified sludge is subjected to combustion at a temperature of 970 ° C in the presence of a mixture of air and a reducing agent - an aqueous solution of ammonia.

The mixture of air and reducing agent is directed into a rotary drum furnace with a linear speed of 13 m / s in two directions - along the course of flue gases in a turbulent mode and perpendicular to their direction from top to bottom.

The specified mixture is fed through the feed channels, which are made in the upper part of the furnace. In this case, a mixture of air and reducing agent, directed into the furnace along the flue gases, is fed through channels with turbulators installed inside them.

The ammonia content in the solution is 10%. Ammonia consumption is 3 g / kg waste.

The product formed as a result of combustion, consisting of slags and flue gases, is subjected to afterburning in an afterburner at a temperature of 1380 ° C for a time of no more than 2 seconds with simultaneous recuperation with a heat transfer coefficient of 45 W / m ² K to obtain the removed ash and slag waste and the first stream flue gas

Water is supplied to the recuperator installed in the afterburner and heat exchange is carried out between the coolant and flue gases through the separating heat transfer surface. The heated coolant is sent to consumers.

The first stream of flue gases is directed to the scrubber, where it is reacted for no more than 2 seconds, initially with dolomite flour in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension and then at a temperature of 185 ° C with a gas purification catalyst located in the lower part of the scrubber. As a sorbent in the form of an aqueous suspension, a mixture in the form of an aqueous suspension of activated alumina, silica gel and NaX zeolite is used at a mass ratio of water: dolomite flour: activated alumina: silica gel: NaX zeolite equal to 1: 0.17: 0.3: 0.3 : 0.9, respectively (the total amount of water contained in aqueous suspensions of dolomite flour and sorbent is taken into account).

Dolomite flour in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension are fed into the scrubber through nozzles installed in its upper part.

The catalyst used is a Filtra DS-90E zinc-based gas purification catalyst (zinc oxide content 90%).

The second flue gas stream formed after passing through the scrubber is subjected to cyclonic cleaning at a temperature of 185 ° C with the formation of cyclonic cleaning waste and a third flue gas stream.

The specified third stream of flue gases is directed to the mixing stage, where it is subjected to contact in a mixer with a powdered sorbent. As a powdered sorbent, a mixture of powdered lime, shale ash, and activated alumina is used with a mass ratio of powdered lime: shale ash: activated alumina equal to 1: 0.25: 0.18. The process is carried out at a temperature of 185 ° C.

In this case, the waste of the mixing stage and the fourth stream of flue gases are obtained, which is sent for cleaning to a bag filter at a temperature of 185 ° C.

The flue gases purified in the bag filter are discharged into the atmosphere, and the waste generated during purification is recycled to the mixing stage, to the mixer.

Example 3.

Use solid household waste of the morphological composition shown in Table 1.

Municipal solid waste is incinerated. The combustion is carried out at a temperature of 1000 ° C in the presence of a mixture of air and a reducing agent - an aqueous solution of urea. The urea content in the solution is 23%, the urea consumption is 2.5 g / kg waste.

The mixture of air and reducing agent is directed for combustion into a rotary kiln at a linear speed of 25 m / s in two directions - along the course of flue gases in a turbulent mode and perpendicular to their direction from top to bottom.

The specified mixture is fed through the feed channels, which are made in the upper part of the furnace. In this case, a mixture of air and reducing agent, directed into the furnace along the flue gases, is fed through channels with turbulators installed inside them.

The product formed as a result of combustion, consisting of slags and flue gases, is subjected to afterburning in an afterburner at a temperature of 1200 ° C, for a time of not more than 2 seconds with simultaneous recuperation with a heat transfer coefficient equal to 60 W / m ² K and the removed ash and slag waste and the first stream are obtained flue gases.

Water is supplied to the recuperator installed in the afterburner and heat exchange is carried out between the coolant and flue gases through the separating heat transfer surface. The heated coolant is sent to consumers.

The first stream is directed to a scrubber, where it is reacted for no more than 2 seconds. initially with limestone flour in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension, which is a mixture of silica gel and zeolite ZSM-5 in the form of an aqueous suspension, with a mass ratio of water: limestone flour: silica gel: zeolite ZSM-5, equal to 1: 0 , 11: 0.7: 0.15 (the total amount of water contained in aqueous suspensions of limestone flour and sorbent is taken into account) and then at a temperature of 200 ° C with a gas purification catalyst located in the lower part of the scrubber.

As a catalyst, a gas purification catalyst FCR-91 is used (the chemical composition is alumina and modifiers 92-95%, SO ₄ / Cl / NO ₂ - less than 0.01%, other metals - less than 0.01%).

Limestone flour in the form of an aqueous suspension and a sorbent in the form of an aqueous suspension are fed into the scrubber through nozzles installed in its upper part.

The second flue gas stream formed after passing through the scrubber is subjected to cyclonic cleaning at a temperature of 200 ° C with the formation of cyclonic cleaning waste and a third flue gas stream.

The specified third stream of flue gases is directed to the mixing stage, where it is subjected to contact in a mixer with a powdered sorbent - a mixture of powdered lime, activated carbon, activated alumina, iron (III) chloride, iron and copper phosphate at a mass ratio of powdered lime: activated carbon: activated aluminum oxide: ferric chloride: copper phosphate equal to 1: 0.12: 0.8: 0.11: 0.2. In this case, contacting waste and a fourth flue gas stream are obtained. The fourth stream of flue gases is directed to a bag filter for cleaning at a temperature of 200 ° C. The flue gases purified in the bag filter are discharged into the atmosphere, and the waste generated during purification is recycled to the mixing stage, to the mixer.

Table 2 below shows the data on the concentration of pollutants in the emissions of flue gases into the atmosphere generated during the processing of waste and subjected to treatment by the described method (examples 1-3) in comparison with similar data on the content of pollutants in the emissions of flue gases that are not subjected to treatment. ...

From the data in the table it follows that the claimed method of waste processing allows, when processing a variety of wastes, including those with a multiple excess of the content of harmful substances in the resulting flue gases generated during the combustion of oily waste, to obtain consistently high results in the processing of waste and cleaning the flue gases generated as a result of the specified processing.

Carrying out the described method, under the conditions specified in the stated intervals, leads to similar results, carrying out this method under conditions outside the stated limits does not lead to the desired results. Carrying out the claimed method using the above-mentioned types of calcium-containing alkaline reagent in the form of an aqueous suspension, a sorbent in the form of an aqueous suspension and a powdered sorbent, the choice of which depends on the type of initial waste, leads to a high degree of purification.

The advantages of the combination of a semi-dry technology for cleaning gases with simultaneous feeding of sorbents in the form of aqueous suspensions into hot flue gases used in the described method are lower investment costs associated with a high degree of purification, reduced energy consumption, lack of effluents, and significantly higher reliability of work.

The claimed method makes it possible to reduce the temperature at the stages of waste incineration in the furnace and the afterburning stage, which leads to a decrease in energy consumption by an average of 20.0-23.0 rel.%, And also makes it possible to increase the degree of flue gas purification by 23.0-25.0 % rel.

Claims (4)

1. A method of waste processing, which consists in the fact that the original waste is incinerated in a drum furnace at a temperature of 900-1000 ° C in the presence of a mixture of air and a reducing agent - aqueous solutions of urea or ammonia, which is sent for incineration into a drum furnace with a linear speed of 6 up to 25 m / s in two directions - along the course of flue gases in a turbulent mode and perpendicular to their direction from top to bottom, the product formed during combustion, consisting of slags and flue gases, is subjected to afterburning at a temperature of 1300-1500 ° C, for a time not more than 2 seconds with simultaneous recuperation with a heat transfer coefficient of 30-60 W / m ² K with obtaining ash and slag waste and the first stream of flue gases, which is sent to the scrubber for cleaning by interaction for no more than 2 seconds, initially with a calcium-containing alkaline reagent in the form of an aqueous suspension and a sorbent in in the form of an aqueous suspension, and then at a temperature of 180-200 ° C with a gas purification catalyst, the resulting second stream d flue gases are subjected to cyclonic cleaning with the formation of cyclonic waste and a third flue gas stream, which is fed to the stage of mixing with a powdered sorbent to obtain a fourth flue gas stream, which is sent to a bag filter for cleaning, the resulting purified flue gases are discharged into the atmosphere, and the resulting flue gases are discharged into the atmosphere. cleaning waste is recycled to the stage of mixing with a powdered sorbent. 2. A method according to claim 1, characterized in that lime, dolomite flour, limestone flour are used as a calcium-containing alkaline reagent in the form of an aqueous suspension. 3. The method according to claim 1, characterized in that shale ash, zeolite, activated carbon, activated alumina, silica gel, activated alumina or a mixture thereof are used as a sorbent in the form of an aqueous suspension. 4. The method according to claim 1, characterized in that a sorbent selected from the group consisting of quicklime, slaked lime, limestone, shale ash, zeolite, dolomite, activated carbon, activated alumina, silica gel, iron hydroxide ( II), magnesium oxide, zinc oxide, cobalt oxide, calcium oxide, iron (III) chloride, copper oxide, copper sulfate, copper phosphate, lead sulfate, lead phosphate, cadmium sulfate, cadmium phosphate, activated aluminum oxide, or a mixture thereof.