GENERATION

BACKGROUND

1. Field

The invention refers to the field of heat engineering and ecological technologies, particularly, to apparatuses for heat energy generation from hydrocarbon fuel (liquid and gaseous) mainly used in systems of water heating and apparatuses for hazardous wastes utilization.

2. Description of Related Art

A known unit for generation of heat from hydrocarbon fuel to heat a water medium comprises a gas-liquid jet device, equipped with: a main nozzle and water inlet connected to the heat carrier (water) outlet in a combustion system; an inlet for combustion products in form of a vapor-gas-water mixture; a blending chamber; a combustion chamber, equipped with a water outlet, connected to the heat carrier outlet of the combustion system; a fuel nozzle and outlet connected to the combustion products inlet of the gas-liquid jet device; a separator, equipped with an inlet connected to the gas- liquid jet device outlet; a water outlet connected to the inlet of the heat consumption system; and a gas outlet. (RU2202055 C2, IPC ⁷ F04F5/54, published 10.04.2003).

The stated known technical solution accepted as a prototype ensures heating of the water heat carrier and its supply to a heating system, but is subject to certain disadvantages. Firstly, the apparatus produces environmental pollution in the form of waste gases such as exiting from the separator. Secondly, the apparatus is not effective for high rates of thermal heating due to providing only relatively low fuel consumption per unit of generated heat power.

SUMMARY

Target of the present invention is to provide such a design of an apparatus for heat generation from hydrocarbon fuels, capable of providing a substantial reduction in specific fuel consumption and minimizing environmental pollution in the form of waste gases. The target is achieved by the following. An apparatus for combustion residue recovering and heat generating incorporates, at least, one transonic jet apparatus with an inlet for active medium (the first inlet), an inlet for passive medium (the second inlet) and an outlet for connecting to an inlet of a gas-water phases separator for the mixture obtained from the transonic apparatus, the said separator incorporates gas and water outlets, which in order are executed with possibility of connection to the lines of harmful impurities recovering found in gas and water phases accordingly, at this the transonic jet apparatus incorporates the main nozzle connected to the inlet for active medium, a nozzle for passive medium (secondary nozzle), and a mixing chamber, at this the nozzle for passive medium is executed in the form of an annular nozzle coaxial with the main nozzle and encircling it, and narrowing from its inlet section to the most narrow one and further expanding to its outlet section.

Water can be used as an active medium, and fuel combustion residue can be used as a passive medium. Another variant, where fuel combustion residue is used as an active medium, and water is used as a passive medium, is also possible.

At this, for the purpose of harmful impurities recovering, for example carbon and sulfur oxides, found in water phase it can be supplied with calcic decarbonator connected to the water outlet of the separator, and with a reservoir for a chemical agent, for example alkali liquor, and a measuring valve connected to the mixing chamber of the jet apparatus and/or to the separator.

The nozzle for passive medium is transonic, and the separator is executed in the form of a cyclone.

In variant of the apparatus execution where water is used as the active medium connection of the active medium inlet of the transonic jet apparatus to the reverse line ("return") of the heat supply system is possible. At this the separator is executed with possibility of connection by the water outlet to the direct line of the heat-supply system

In this variant (with water as the active medium) the main nozzle can be executed in the form of the Fisenko nozzle, which includes an inlet convergent and an outlet divergent along the medium flow sections. At this the inlet section is executed with multistage draw-down of the inner diameter with possibility of boiling of a part of the stream. And the geometric profile of the divergent outlet section of the nozzle is formed by the part of a concave towards the axis of the nozzle part of the curve transiting smoothly into a convex part. At this the critical section of the nozzle where the stream velocity is equal to the sound velocity is located in the outlet section of the nozzle. At this the best result is reached under condition when the smooth and continuous transition of the concave part into the convex part is located in a critical section of the nozzle, where the second-order derivative of the section area along the nozzle length is equal to zero. Further, the transonic jet apparatus can have a sharp edge located in the inlet section. Further, the concave part of the outlet section of the main nozzle can have a profile of its initial part characterizing by sudden enlargement of its diameter from the inlet of the outlet section of the nozzle along the stream flow, at this the first-order derivative from the area of the cross-section of the outlet part on coordinate along the axis has a maximum value on the inlet to the concave part. The profile of the outlet section of the main nozzle in the transonic jet apparatus is executed close to the form of the stream profile calculated according to equation of reversible adiabat linking the current diameter of the nozzle with the current thermodynamic parameters of the stream for the set input parameters of temperature and pressure and with account of the adiabatic index k _p for the homogenous two-phase mixture. At this the adiabatic index k _p characterizes gas-liquid, for example vapour-water mist-like medium, the sizes of particles of which are smaller than the length of their free run and determined from the relationship

where 0.5 < β _ρ < 1 characterizes the volume ratio of gaseous phase in the flow of gas-liquid (vapour-water) medium in the critical section of the nozzle.

The transonic jet apparatus of the applied apparatus can include as additional nozzle connected to the mixing chamber. At this, the additional nozzle is executed in the form of the Fisenko nozzle of the above-described design. Namely, it includes an inlet section executed in the form of a cylindrical channel connected to the outlet divergent section. At this, the outlet section has geometric profile formed by the part of a concave towards the axis of the nozzle part of the curve transiting smoothly into a convex part. At this the critical section of the nozzle where the stream velocity is equal to the sound velocity is located in the outlet section of the nozzle. Further the outlet section of the additional nozzle of the transonic jet apparatus can include an outlet cylindrical part connected to the convex part of the outlet section. At this, the best result is reached under condition when the continuous transition of the concave part into the convex part is located in a critical section of the nozzle, where the second-order derivative of the section area along the nozzle length is equal to zero. The cylindrical part of the additional nozzle can have the length of 0,5 to 1 its diameters. Besides, the positive effect on achievement of the result can be made by presence of a sharp edge in the transonic jet apparatus; the said sharp edge is located in the zone of connection of the mixing chamber to the cylindrical channel; and also executing the concave part of the outlet section of the additional nozzle with the profile of its initial part characterizing by sudden enlargement of its diameter from the inlet of the outlet section of the nozzle along the stream flow. At this the first-order derivative from the area of the cross-section of the outlet part on coordinate along the axis has a maximum value on the inlet to the concave part. The profile of the outlet section of the additional nozzle is executed close to the form of the stream profile calculated according to equation of reversible adiabat linking the current diameter of the nozzle with the current thermodynamic parameters of the stream for the set input parameters of temperature and pressure and with account of the adiabatic index k _p for the homogenous two-phase mixture, which prevails in composition of mixed water medium and gaseous discharge incorporating harmful impurities, for example end products of fuel combustion. In this case the adiabatic index k _p characterizes gas-liquid (including vapour-water) mist-like medium, the sizes of particles of which are smaller than the length of their free run and determined from the relationship k = 0.592 ₊ ^2§?

β,

where 0.5 < β _ρ < 1 characterizes the volume ratio of gaseous phase in the flow of gas-liquid (vapour-water) medium in the critical section of the nozzle.

In variant of the apparatus execution with the additional nozzle having profile of the Fisenko nozzle, the Laval nozzle can be used as the main one.

The applied apparatus can include the second transonic jet apparatus with the above-mentioned variant of its execution (where the main nozzle is the Laval nozzle of the Fisenko nozzle); at this the second apparatus is connected to the separator from the opposite to the first one side with possibility of unidirectional rotation of streams from the first and second apparatuses. Further, the separator can incorporate a heat exchanger connected to the independent circuit for heating the medium flowing through it.

Further, the apparatus according to the present invention is supplied with an oxygen source connecting to the inlet of the combustion chamber. The oxygen source is executed mainly in the form of an oxygen container. A heat consumption system can be executed either in the form of a hot-water radiator or in the form of a heat exchanger for water heating of a hot-water supply system, or in the form of a heat exchanger of a hot-water heating system, or in the form of a heat exchanger of a hot-ear heating system.

A method of operation of apparatus for combustion residue recovering and heat generating may comprise of passing an active medium supplied to a first inlet of a transonic jet module through a main nozzle into a mixing chamber. Simultaneously a passive medium is supplied to a second inlet of the transonic jet module and is being passed through a secondary nozzle into the mixing chamber also. The secondary nozzle is an annular converging-diverging nozzle coaxial with and encircling the main nozzle. After that a mixture of the active medium and the passive medium from the mixing chamber is being discharged from an outlet of the transonic jet module into a gas-liquid phase separator. A gaseous product stream is being recovered from a gas outlet of the gas- liquid separator and a liquid product stream is being recovered from a liquid outlet of the gas-liquid separator.

The method might have modification where the active medium consists essentially of water supplied in a liquid form at the first inlet, and the passive medium consists essentially of a fuel combustion residue supplied as a vapor-gas-liquid mixture at the second inlet. Another modification of the method uses the active medium as a essentially fuel combustion residue supplied as a vapor-gas-liquid mixture at the first inlet, and the passive medium as essentially water supplied in a liquid form at the second inlet.

The method may also be modified to further include capability to remove carbonic impurities from the liquid product stream, using a decarbonator coupled to the liquid outlet of the gas-liquid separator. There is possibility to dispense a chemical material to at least one of the mixing chamber or the gas-liquid separator via a dispensing valve. When the passive medium is passing the secondary nozzle it causes transonic flow to occur in the secondary nozzle.

Furthermore the mixture from mixing chamber could be discharged through a third nozzle coupled to the mixing chamber, the third nozzle includes a cylindrical inlet section coupled to a divergent outlet section, wherein the outlet section has a concave profile relative to a central longitudinal axis of the nozzle in an initial portion just downstream of the inlet section that smoothly transitions to a convex profile at a critical section of the nozzle located in the outlet section, the critical section being defined by a transonic stream velocity. The method also includes possibility of mixing the primary medium and the secondary using a second transonic jet module coupled to the gas-liquid separator opposite to the first transonic jet module, and discharging the mixture to cause unidirectional rotation of a gas-liquid mixture admitted to the gas-liquid separator.

A fluid medium could be heated in the gas-liquid separator using a heat exchanger coupled to an independent circuit.

The method also includes boiling the active medium in a convergent inlet section of the main nozzle using a sharp-edged multistage reduction of inner diameter, and expanding the active medium in the divergent outlet section of the main nozzle using a concave profile relative to a central longitudinal axis of the main nozzle in an initial portion just downstream of the inlet section that smoothly transitions to a convex profile at a critical section of the main nozzle located in the outlet section where the active medium reaches a transonic stream velocity. BRIEF DESCRIPTION OF THE DRAWINGS

The present apparatus design is explained by the drawings

Fig.l represents a scheme of an apparatus, in which water is used as the active medium.

Fig.2 represents a longitudinal section of the transonic gas-liquid jet apparatus with the main nozzle in the form of the Fisenko nozzle.

Fig.3 represents a scheme of an apparatus, in which end products of fuel combustion are used as the active medium.

Fig.4 represents a longitudinal section of the transonic jet apparatus with the main nozzle in the form of the Laval nozzle and with additional nozzle in the form of Fisenko nozzle.

DETAILED DESCRIPTION The apparatus, which scheme is represented in firg.l, includes a combustion chamber 1, a transonic gas-liquid jet apparatus 2, a gas path 3, a perforated collector 4, a fuel spray nozzle 5, a separator executed in the form of a cyclone 6, pumps 7, 8 and 9, a regulator 10 incorporating a variable valve, an automatic valve 11, a calcic decarbonator 12, a reservoir 13 with an alkali liquor, a measuring valve 14, and an oxygen container 15.

The combustion chamber 1 is mainly executed cylindrical and has a water inlet connected through the pumps 7 and 8 to the heat carrier outlet from the heat consumption system; the said inlet is executed in the form of an annual perforated collector 4 for feeding water in the sprayed state along the walls of the combustion chamber 1. Further the combustion chamber 1 includes a fuel spray nozzle 5, and an outlet connected to the inlet of the jet apparatus 2 for combustion products, which are vapour-gas-water mixture.

The jet apparatus 2 has a main (water) nozzle 17 executed in the casing 16 (fig.2) and having a water inlet connected to the heat carrier outlet from the heat consumption system; further the jet apparatus 2 has an inlet form combustion products and a mixing chamber 18. The inlet for combustion products of the jet apparatus 2 is supplied with a transonic annular nozzle 19 coaxial with the main nozzle 17 and encircling it. The nozzle 19 narrows from its inlet section to the most narrow one and further expands to its outlet section.

The main nozzle 17 has a narrowing section 20 executed with multistage drawdown of the diameter and an outlet divergent section 21 with the geometric profile formed by the part of a concave towards the axis of the nozzle part of the curve transiting smoothly into a convex part. The nozzle 17 also has a sharp edge 22 located in the inlet section.

The cyclone 6 has an inlet connected to the outlet of the jet apparatus 2, a water outlet connected to the heat carrier inlet to the heat consumption system, and a gas outlet, through which the gas path 3 is connected to the inlet to the combustion chamber 1. The oxygen container 15 is connected to the gas path 3.

Fig 1 also shows a straight pipe for feeding water into the heat consumption system, a reverse pipe ("return") for water return from the heat consumption system, a launch line connecting the cyclone 6 with inlet of the jet apparatus 2 through the pumps 7 and.8, a pipe for water feeding into the cyclone 6 (additional feeding).

The apparatus, which scheme is shown in fig. 3, includes the first transonic jet apparatus 23 and the second transonic jet apparatus 24 both connected to the separator from the opposite sides with possibility of unidirectional rotation of streams from the first and the second apparatuses. At this, the separator is executed in the form of the cyclone 6.

The cyclone 6 in this apparatus includes a heat exchanger 26 connected to the independent circuit for heating the medium flowing through it. This cyclone has a gas outlet 26 and a water outlet 27 connected through the pump 28 to the line of recovering of harmful impurities found in the water phase.

Further a calcic decarbonator 12 is connected to the cyclone 6 (fig. 3) by means of the circulation pipeline 29 supplied with a pump 30.

A line 33 for pure water feeding is connected to the inlets 31, 32 for passive mediums of the jet apparatuses 23, 24.

The jet apparatuses 23, 24, which longitudinal section is shown in fig. 4, include the main nozzle 34 for active medium (for example combustion products) executed in the form of the Laval nozzle, an annular nozzle (the second nozzle) 35 for water used as a passive medium, a mixing chamber 36, an additional nozzle (the third nozzle) 37 with the inlet section executed in the form of a cylindrical continuation of the channel 38 with length from 0,5 to 1 its diameters connected to the outlet divergent section.

The jet apparatuses 23, 24 have a sharp edge 39 located in the zone of the mixing chamber 36 connection to the cylindrical channel 38. The additional nozzle 37 executed in the form of the Fisenko nozzle has a profile of the outlet section the same as the main nozzle 17 in the apparatus, which scheme is shown in fig.l, has. Namely, the geometrical profile of the divergent outlet section of the nozzle is formed of the nozzle's part 40 concave towards the axis of the nozzle, which smoothly changes into the convex one 41, at this the critical section 42 of the nozzle where the stream velocity is equal to the sound velocity is located in the outlet section 37 of the nozzle. The outlet section of the additional nozzle 37 also has an outlet cylindrical part 43 connected with the concave part

41 of the outlet section.

The apparatus according to the present invention in variant represented in figs. 1 and 2 operates as follows. Oxygen is used as an oxidizing compound for fuel combustion in the apparatus; however, air inhausted from the atmosphere can also be used. In this case the amount of oxygen necessary for the apparatus launch can be fed from the oxygen container 15 to accelerate the launch.

Oxygen from the container 15 is fed into the gas path 3, hot water is fed into the perforated collector 4 to create a vapour-water screen along the walls of the combustion chamber 1, and fuel (gas or liquid fuel or water-fuel emulsion) is fed to the fuel spray nozzle 5 and burnt.

The contact heating of vapour-water mixture by a gas flame is realized in the combustion chamber 1. At this gas is cooled to the temperature of saturated vapour with temperature of about 100°C. Vapour-gas-water mixture is fed to the jet apparatus 2 where it is accelerated to the supersonic velocity in the annular nozzle 19, mixed with boiling water, which is fed through the main nozzle 17 from the cyclone 6, then the said mixture is decelerated in the pressure sudden change on the outlet from the jet apparatus 2 and is fed into the cyclone 6 with subsonic velocity. Process of water boiling in the jet apparatus 2 occurs as follows. Hot water stream with the set parameters of pressure and temperature is fed to the inlet section 20 of the nozzle 17 in which it flows with constants in velocity and pressure before step change of the internal diameter, i.e. transition to the outlet section 21 through a cylindrical part. As a result of step narrowing in the inlet section of the nozzle velocity of the stream increases, pressure of water in the stream falls that is strengthened by separation of the stream from a sharp edge 22. As a result at achievement of pressure of saturation at the set temperature boiling of the hot water stream occurs that leads to formation of two-phase vapour-water medium in narrow section. At this, the stream density decreases, velocity increases and acceleration of the hot vapour-liquid stream in the inlet section of the nozzle occurs. Then the vapour-liquid stream from the inlet section is fed to the outlet section 21 of the nozzle. In a concave part of the diverging outlet section 21 of the nozzle further increase of the vapour-liquid stream velocity occurs, and it reaches local sound velocity and is fed to a convex part of the outlet section 21 of the nozzle where further acceleration of the stream occurs.

In the beginning of the outlet section 21 of the nozzle 17 the stream represents a liquid with microscopic bubbles of vapour, which being the vapour generating centers provide volume boiling of liquid in process of pressure decrease in the two-phase stream. The outlet section 21 of the nozzle 17 has a geometrical profile, in which the two-phase medium flows without separation of the stream from the nozzle walls. This profile is executed approaching to the stream profile shape calculated according to equation of reversible adiabat linking the current diameter of the nozzle with the current thermodynamic parameters of the stream with account of the adiabatic index k _p for the homogenous two-phase mixture. Vapour generating is continued in the outlet section 21, because of it the density of the mixture decreases, velocity of the stream grows, and the sound velocity decreases. In some section (in critical section of the nozzle) velocity of the stream becomes equal to the sound velocity, and the stream becomes critical. At this medium with microscopic bubbles of vapour is transformed into the mist-like medium which sizes of particles are smaller than length of their free run. Further its expansion occurs with the supersonic velocity. On the outlet from the divergent part of the outlet section 21 of the nozzle 17 velocity reaches maximum. Therefore, the stream with supersonic velocity arrives in the outlet from the nozzle 17. At this an intensive conversion of liquid internal energy into kinetic energy of the stream occurs. Kinetic energy of the stream can be converted into heat energy in pressure sudden change which is organized downstream the outlet section of the nozzle. For this purpose the nozzle 17 can additionally be supplied with the cylindrical part connected to the convex part of the outlet section 21. In the jet apparatus 2 the cylindrical mixing chamber 18 acts as such a cylindrical part.

Separation of liquid and gas phases occurs in the cyclone 6. Water from the cyclone 6 is fed to the consumer by means of the pump 9, and then the cooled water is fed through the reverse pipe ("return") of the heat consumption system to the water nozzle of the jet apparatus 2 and partially to the perforated collector 4. Maintaining of necessary oxygen concentration in the process of combustion is realized by means of the control device 10 executed in the form of variable door-valve.

In case of perfect combustion of the hydrocarbon fuel in oxygen there appear the combustion products: steam, and carbon dioxide. The following physical-chemical processes occur with combustion products.

After mixing with boiling water in the jet apparatus 2 and deceleration in pressure sudden change steam formed in the process of fuel combustion is condenses. At this, heat of vapour generating is released and fed to the heat consumer.

This heat of vapour generating is an additional heat relating to the fuel lower heating value according to which efficiency of apparatuses for heat energy generating is measured. Due to the said heat of vapour generating utilization coefficient of the fuel use in the apparatus according to the present invention will exceed 1.

First carbon dioxides will be partially absorbed with water in the jet apparatus 2, and then will be wholly absorbed in the calcic decarbonator 12. At this the absorption heat is released as well as the heat at chemical transformation of lime into calcium carbonate. These heats will also be additional to the fuel combustion heat.

The control device 10 maintains the preset pressure in the gas path 3. Intensity of gas emission in the jet apparatus 2 and gas composition in the combustion chamber 1, and combustion efficiency of hydrocarbon fuel, and intensity of additional heat generation at water condensing and carbon dioxides absorption depend on this pressure. In case of overpressure discharge of excess amount of gas and some amount of steam into environment is realized. In case of lack of oxygen on the outlet from the combustion chamber 1 CO content increases. In this case it is necessary to take steps for oxygen feeding increase, and if increase of oxygen feeding is impossible to stop fuel feeding into the combustion chamber 1 and take a close look at the reasons of decrease of oxygen feeding.

In process of absorption of carbon dioxide and combustion products in the mixing chamber 18 carbonic acid appears, and accordingly pH index of water fed into the cyclone 6 is changed. Processes carbon dioxide of desorption in the cyclone 6 and water decarbonation in the calcic decarbonator 12 depend on this index.

In case of low pH index value due to carbon dioxide desorption in the cyclone 6 pressure in the gas path 3 will increase that can lead to discharge of combustions products through the control device 10 into environment. Depending on the pH index value, with account of pH decrease due to formation of carbonic acid, when it reaches a preset value alkali from the reservoir 13 with alkali liquor is fed into the mixing chamber 18 of the jet apparatus 2 through the measuring valve 14, forming salt and water in interaction with carbonic acid and at the same time increasing pH to the set value. In this case water decarbonization without pressure increase in the gas path 3 and without carbonate dissolving in the calcic decarbonator 12.

Upon results of already conducted experiments, it was possible to reduce the specific fuel consumption per unit of produced heat power by no less than 10%, and under optimal conditions this reduction can be no less than 15%. Creation of a compact, efficient, and ecologically sound unit for water heating and hot water supply systems, which at oxygen use as an oxidizing compound slightly discharge carbon dioxide into environment, was finally achieved. In case of air use as an oxidizing compound some carbon dioxide formed at hydrocarbon fuel combustion is discharged into atmosphere along with nitrogen, because in this case carbon dioxide in combustion products is diluted by air components (nitrogen and argon), which do not take part in fuel combustion.

Big volume of combustion products in air and low concentration of harmful gases

(carbon and sulfur dioxides) in them cannot allow using water as an active medium in the apparatus for combustion residue recovering and heat generating as very big water discharge will be required for operation of jet apparatuses.

For combustion residue recovering in air the apparatus shown in fig. 3 can be used. It operates as follows.

Hot combustion products under pressure exceeding the atmospheric pressure are fed to the inlets for active medium and into the main nozzles of the jet apparatuses 23, 24; and cold water purified of harmful impurities incorporated in combustion products is fed to the inlets 31, 32 for passive medium.

Combustion products are accelerated to the supersonic velocity in the nozzle 34 executed in the form of the Laval nozzle; and water is accelerated in the annular nozzle 35. In the mixing chamber 36 streams of water and combustion products are mixed with formation of gas-liquid mixture.

At this water is heated by the hot combustion products and partially evaporates with formation of vapour-gas mixture with drops of water. In the mixing chamber 36 and especially in the zone of connection of the chamber 36 with the cylindrical channel 38 sudden changes of compacting appear, gas-liquid stream is decelerated in them and pressure in the said stream increases.

In the areas of increased pressure appeared due to sudden changes of compacting, vapour formed at heating and evaporating of water condenses, and harmful impurities (carbon and sulfur dioxides) are partially dissolved in water. To increase carbon and sulfur dioxides dissolvability in water alkali liquor may be fed into the chamber 36 all the same as it is in the apparatus, which scheme is shown in fig.l.

Stream separation from the walls of the cylindrical channel 38 occurs on the sharp edge, and pressure in the stream decreases. Due to this water in drops heated in the mixing chamber 36 adiabatically boils, and microscopic vapour bubbles are formed in the drops.

When gas-liquid stream is fed into divergent section 37 of the nozzle adiabatic boiling of water in drops is continued due to pressure decrease at the stream expansion. As a result gas-liquid stream is accelerated to supersonic velocity with formation of homogenous mist-like medium, the sizes of particles of which are smaller than the length of their free run. This process is similar to the one occurring in the nozzle 17 at operation of the apparatus shown in fig.l.

Great amount of small drops in the mist-like medium have big surface for contact between gas and water that assists carbon and sulfur dioxides dissolving in water. At the stream discharge from the nozzle 37 into the cylindrical channel 43 the stream in this channel is decelerated to subsonic velocity with formation of sudden change of compacting, in which pressure increases.

Due to pressure increase in the sudden change of compacting carbon and sulfur dioxides are additionally dissolved in small water drops in the mist-like medium or in alkali liquor drops if such a liquor has been fed into the mixing chamber 36. At this, in the sudden change of compacting vapour is partially transformed into gas-liquid medium with big water drops, which can contain small vapour bubbles.

At gas-liquid stream discharge to the cyclone 6 from one or two jet apparatuses 23, 24 the stream rotating along the walls is formed in the cyclone, separation of gas from liquid occurs in this stream due to centrifugal force. Gas partially purified of carbon and sulfur dioxides is deleted from the cyclone 6 through the gas outlet 26.

Water with carbon and sulfur dioxides dissolved in it comes down along the walls of the cyclone 6 and is removed from it through the water outlet 27 be means of the pump 28 into the line for utilization of harmful impurities found in water. At this processes similar to those in the cyclone 6 operating in the apparatus shown in fig.l occur in water.

To reduce carbon and sulfur dioxides desorption it is also possible to increase pH for liquid medium by adding alkali liquor and partially purify water of carbon and sulfur dioxides by means of its pumping by the pump 30 along the circulating pipeline 29 through the calcic decarbonator 12.

To reduce carbon and sulfur dioxides desorption from water in the cyclone 6 water is cooled be means of the heat exchanger 25 connected to an independent consumer. When pressure in the cyclone 6 is close to the atmospheric temperatures of gas and water after their separation will be close to the dew-point temperature which can be, for example, 60-70°C.

Heat carrier in the heat exchanger 25 can be heated up to this temperature.

However, to improve the process of harmful impurities removal from combustion products cold water can be fed into this heat exchanger for cooling gas-liquid mixture in the cyclone 6. In this case heat generation in the apparatus will decrease and degree of combustion products purification from harmful impurities will increase.

In the apparatus shown in fig. 3 heat incorporated in combustion products is effectively transformed into kinetic energy of gas-liquid stream, which is spent for formation of a mist-like medium with a big surface for water and gas contact. This assists to harmful impurities dissolving in water.

Therefore, the applied apparatus can be used for utilization of gaseous discharges (vapour and/or gas mixtures) incorporating harmful impurities both connected with burning and not connected with it. At this the best application the applied apparatus will meet in utilization of combustion products of heat power plants (coal, gas, residual, peat coal, working on organic fuel, etc.), boiler plants, big internal-combustion engines' exhausts, and also automobiles exhausts. Besides, the apparatus can be applied at utilization of combustion products at metal fabrication. Use of the applied invention allows solving a group of problems, i.e. utilize discharges incorporating harmful impurities, obtain heat while utilization and further useful use of this heat, and also obtain marketable products from the utilized products.