RU2446195C1 - Method of producing low-dispersed technical carbon and reactor for realising said method - Google Patents

Abstract

FIELD: chemistry.

SUBSTANCE: invention relates to production of technical carbon from liquid hydrocarbon material via thermal-oxidative decomposition. The method of producing low-dispersed technical carbon involves mixing fuel with hot process air, complete combustion of the fuel mixture in a cyclone-type combustion chamber (2) to form a stream of flue gases which revolves and moves down axially, enters a mixing zone (3), mixing the fuel gas with hydrocarbon material fed into the mixing zone (3) through a nozzle (12), feeding the formed stream of hydrocarbon-gas mixture into an evaporation chamber (4) into which hot process air is tangentially fed through channels (14), said air being swirled in a direction opposite the direction of rotation of the stream of flue gases, evaporating the mixture, feeding the stream of the formed hydrocarbon vapour into a reaction chamber (6), where it undergoes thermal-oxidative decomposition in a pyrolysis zone (7) to form an aerosol of technical carbon, and further cooling in a cooling zone (7) by spraying cooling water through a nozzle (15).

EFFECT: invention enables optimisation of expenses particularly on energy resources while ensuring efficient operation of the reactor with high output and stable quality of the obtained product, as well as reduction of overall dimensions, increasing reliability and service life of the reactor.

7 cl, 1 dwg, 1 tbl

Description

Technical field

The invention relates to the production of carbon black from liquid hydrocarbon by thermo-oxidative decomposition (pyrolysis), in particular, to methods, as well as to devices for producing low-dispersed (low-activity and semi-active) carbon black.

State of the art

A known method of producing a low-dispersed (inactive) carbon black, comprising the formation of a fuel mixture by burning part of the liquid hydrocarbon feed to the reactor, or the combustion chamber of a multi-furnace furnace by mechanical nozzles. In this case, another part of the atomized hydrocarbon feed is vaporized and, subject to a lack of oxygen, is thermally decomposed to form solid particles of low-dispersed carbon black. To ensure the combustion of hydrocarbons, air is supplied to the reactor or furnace through special slit openings that provide mixing with burning drops of hydrocarbon feed. In addition, in the lining of the reactor (multi-furnace) provide for the organization of the supply of additional air to the reaction zone to control the physicochemical properties of the resulting carbon black. In this case, the amount of air entering the reactor is provided by controlling the vacuum level in the reactor (furnace), provided by a smoke exhauster installed after the reactor (furnace) before supplying the carbon black aerosol to the electrostatic precipitator to capture the resulting carbon black [V. Zuev, V. Mikhailov AT. “Soot production”, Moscow, 1970, pp. 152-155). In the described method there are no necessary technological methods for maintaining a stable mode (temperature in the reaction zone, air consumption for burning liquid raw materials and soot formation conditions), atmospheric air is used without its preliminary heating. The disadvantage of this method is its low efficiency due to the combustion of part of the raw material and its incomplete decomposition. In addition, part of the hydrocarbon feed remains on the surface of the resulting carbon black, which leads to a deterioration in the quality of the product and environmental damage.

Closest to the claimed method is a method for producing low-dispersed [low-activity and semi-active) carbon black from liquid hydrocarbon raw materials by thermo-oxidative decomposition in a vertical reactor, including preliminary heating of liquid hydrocarbon raw materials to a temperature of 150-200 ° C, process air due to regenerative heat exchange with aerosol carbon black to a temperature of 450-650 ° C, mixing fuel with heated process air with an excess air ratio of 1.2-1.3, RGANIZATION complete combustion of the fuel mixture in the combustion zone at a temperature of 1540-1700 ° C to obtain a flue gas with residual active oxygen at the rate of complete fuel combustion of residual air quantity 0.4-1.0 ^Nm3 / kg of hydrocarbon feedstock, mixing the hydrocarbon feed in the flue gas stream, the evaporation of hydrocarbon feedstock, its thermo-oxidative decomposition with the formation of a carbon black aerosol in the reaction zone for a time of 2-3 s at a temperature of 1260-1330 ° C, its preliminary cooling by injection Single chemically purified water and its subsequent cooling (RU 2317308 C1, published 20.02.2008).

One of the serious drawbacks of the prototype method for producing low-dispersed [low-activity and semi-active] carbon black is the possibility of producing carbon black with parameters different from the requirements of the specification, and above all, in terms of dispersion. Another disadvantage is the possibility of grit formation. In addition, part of the hydrocarbon feed remains on the surface of the resulting carbon black, which leads to a deterioration in product quality.

The objective of the present invention is to intensify the process of producing low-dispersed [low-activity and semi-active] carbon black, reduce the possibility of grit formation, increase the yield of carbon black in terms of indicators meeting the requirements of the international specification ASTM D1765 and GOST 7885-86.

Disclosure of invention

The problem is solved due to the fact that in the method of producing low-dispersed (low-activity and semi-active) carbon black from liquid hydrocarbon raw materials by its thermo-oxidative decomposition in a vertical type reactor, including preliminary heating of liquid hydrocarbon raw materials to a temperature of 150-200 ° C, heating of the process air for account of recuperative heat exchange with a carbon black aerosol to a temperature of 450-650 ° C, mixing fuel with heated process air with an excess coefficient of air 1.2-1.3, the organization of complete combustion of the fuel mixture in the combustion zone at a temperature of 1540-1700 ° C to produce flue gas with residual active oxygen, based on the calculation of complete combustion of the fuel by the amount of residual air 0.4-1.0 nm ³ per 1 kg of hydrocarbon feedstock, mixing hydrocarbon feedstock in a flue gas stream in the mixing zone, evaporation of the hydrocarbon feedstock, its thermal oxidative decomposition (pyrolysis) with the formation of carbon black aerosol, preliminary cooling by injection of chemically purified water and its last Catering cooling introduced distinctive features, which are as follows.

The method is carried out in a reactor claimed according to claim 4, in which the combustion chamber, the mixing zone and the evaporation chamber are in the vertical part of the reactor, and the pyrolysis zone and the preliminary cooling zone are in the horizontal part of the reactor (reaction chamber), wherein the mixtures are organized in a cyclone-type combustion chamber with the formation of a flue gas stream rotating at a tangential velocity near the wall of 20-50 m / s, moving axially downward at a speed of 0.6-1.0 m / s and entering the mixing zone with an increase soon ty to 1.1-1.5 m / s, achieved by reducing the cross section in the mixing zone, where hydrocarbons are fed into the rotating flue gas stream with several jets, provided that the ratio of the feed speed and the tangential velocity of the flue gas in the injection zone 1 (2 ÷ 4), then the resulting flow of the hydrocarbon-gas mixture through the diffuser enters the evaporation chamber, into which low-pressure air preheated to a temperature of 450-650 ° C is tangentially fed, swirling in the direction opposite to the direction of rotation of the smoke stream gas, ensuring the operating temperature in the evaporation chamber of 1400-1650 ° C, then the flow of hydrocarbon vapor with an increase in axial velocity to 9-14 m / s due to an increase in its volume and a narrowing of the evaporation chamber passing into the vertical channel passes to the chamber reactions, which enter with a decrease in speed to 8.5-13 m / s due to an increase in diameter by 1.1 times, and where the temperature of 1240-1360 ° C is set in the pyrolysis zone and its residence time of 0.8-4 s is ensured.

To obtain semi-active carbon black, hydrocarbon feed is introduced radially using pneumomechanical nozzles.

To obtain inactive carbon black, hydrocarbon feed is introduced at an angle of 90 ... 170 ° relative to the tangential velocity vector of the rotating flue gas flow using mechanical nozzles.

The implementation of the method according to the invention.

Figure 1 shows a method of producing a low dispersed carbon black, which is implemented in a reactor, including:

- the vertical part (housing) 1 consisting of: a combustion chamber 2, a mixing zone 3, an evaporation chamber 4, a vertical channel 5;

- horizontal part (reaction chamber) 6 consisting of: pyrolysis zone 7 and cooling zone (quenching) of carbon black aerosol 8.

The technological process in the reactor begins with the combustion zone, where, in limited volumes of the combustion chamber 2, the fuel is completely burned in the presence of technological air preheated to a temperature of 450-650 ° C using 4 diffusion tangential burners that provide intensive rotation of the combustion products of natural gas with tangential velocity near the wall of the combustion chamber in the range of 20-50 m / s, depending on the amount of fuel, hydrocarbon feed and the grade of carbon black obtained. The coefficient of excess air in the combustion chamber is set within 1.2-1.3 in order to exclude the possibility of increasing the operating temperature in the combustion chamber above 1700 ° C, which ensures reliable and long-term operation of the dome dome of the reactor cover. The diameter of the combustion chamber is 2940 mm. The rotating flue gas flow resulting from combustion moves downward with an axial speed of 0.6-1.0 m / s and reaches mixing zone 3, made in the form of a mixing nozzle with a conical confuser and diffuser. Radial pneumomechanical nozzles are installed in the critical section (throat) of the nozzle, which provide a fine atomization for supplying hydrocarbon raw materials upon receipt of semi-active carbon black of grade N550, N650, N660, or mechanical nozzles for supplying hydrocarbon raw materials upon receipt of low-active carbon black of grade P803, P701. In this case, the nozzle tip of the mechanical nozzle is set at an angle of 90-170 ° relative to the tangential velocity vector of the rotating flue gas stream. The diameter of the nozzle neck is 2400 mm, which ensures an increase in the axial velocity of the flue gases and the hydrocarbon feed introduced into the stream to 1.1-1.5 m / s with a slight hydraulic resistance in the range of 1.0-1.5 kPa. The high resulting (tangential and axial) speed eliminates the possibility of dropping hydrocarbon feed droplets onto the inner surface of the nozzle and eliminates the possibility of grit formation in the zone of introduction of hydrocarbon feed into the reactor. Next, the resulting flow of the hydrocarbon-gas mixture through the diffuser enters the evaporation chamber 4, the diameter of which is equal to the diameter of the combustion chamber. To ensure complete evaporation, technological air preheated to a temperature of 450-650 ° С is introduced tangentially into the lower part of the evaporation chamber, the amount of which corresponds to the hydrocarbon feed rate and the grade of carbon black obtained at the reactor. In this case, the direction of rotation of the process air introduced into the evaporation chamber is opposite to the direction of rotation of the flue gas stream formed in the combustion chamber. This turbulizes the movement of gas flows, which leads to an intensification of heat and mass transfer processes and a decrease in the remainder of undecomposed raw materials on the surface of the emerging nuclei of carbon particles. Next, the hydrocarbon vapor together with the nuclei of the carbon particles through the vertical channel 5 enters the horizontal reaction chamber 6, in which in the pyrolysis zone 7 the required conditions are created [operating temperature, residence time] corresponding to the parameters of the obtained carbon black brand. From the pyrolysis zone, the carbon black aerosol enters the cooling zone [quenching], where the soot formation reactions end by abrupt cooling of the carbon black in order to achieve the required parameters according to the international standard specifications ASTM D1765 or GOST 7885-86. To achieve the required universality of the design in terms of dispersion of the obtained carbon black in the cooling zone 8, preliminary quenching is provided, which allows to reduce the residence time of hydrocarbons in the pyrolysis zone.

Examples of the implementation of this method of producing carbon black are given in the table below.

Table No. p / p Parameter Name Units rev. Carbon black brand P803 N762 N650 N550 one 2 3 four 5 6 7 I Mode parameters one. Hydrocarbon consumption kg / hour 4500 4450 4200 4000 2. Natural gas consumption nm ³ / hour 380 410 440 500 3. Process air flow into the combustion chamber nm ³ / hour 4400 4800 5200 6000 four. High pressure air consumption for spraying raw materials nm ³ / hour - - 1100 1200 5. Consumption of chemically purified water for cooling a carbon black aerosol kg / hour 3800 4100 4400 4600 6. Process air flow into the evaporation chamber nm ³ / hour 1800 2100 2500 2900 II Technological parameters one. Temperature in the combustion zone ° C 1570 1620 1650 1680 2. Evaporation Chamber Temperature ° C 1420 1570 1600 1640 3. The temperature in the reaction chamber ° C 1240 1280 1320 1360 four. Carbon black aerosol temperature in the quenching zone ° C 750 750 800 800 5. Process air preheating temperature ° C 450 550 600 640 6. The tangential speed of rotation of the flue gases in the combustion chamber m / s 25 32 41 49 7. Raw material pressure in front of a mechanical nozzle MPa 1,6 1.4 - - 8. Axial velocity of combustion products in the mixing zone m / s 1,0 1.12 1.3 1.48 9. The residence time of hydrocarbon vapors in the pyrolysis zone from 3,5 2.0 1,5 0.8 10. Specific consumption of residual air per 1 kg of hydrocarbon feed nm ³ / kg of raw material 0.53 0.63 1,03 1,275 eleven. Carbon black yield % 68 66 65 64

Table continuation III Physicochemical parameters of carbon black one. Iodine Adsorption mg / g - 27 36 42 2. Nitrogen adsorption specific surface area m ² / g twenty 29th 36 40 3. Dibutyl Phthalate Adsorption cm ^3/100 g 81 65 120 123 four. Screenings on the grid
- 0.5 mm
- 0.14 mm %
% 0.001
0.01 OTC 0.005 OTC 0.01 OTC 0.01 5. Light transmission of toluene extract not less % 80 85 86 92

Achievable technical result

An advantage of the proposed method is the possibility of obtaining low dispersed carbon black of various grades, both inactive and semi-active, while reducing energy intensity. The technological process for producing carbon black, proposed according to the invention, allows optimizing technological costs in terms of energy resources, ensuring the sufficiency of the process parameters while ensuring the required quality of carbon black.

Description of the prior art for the device

As a prototype, a reactor was selected for producing low-dispersed grades of carbon black of the OZTU design (V.I. Ivanovsky. Carbon black. Processes and apparatuses: Textbook. - Omsk: Tehuglerod OJSC, 2004, p.52-53). The reactor is an apparatus comprising a vertical cylindrical body with a water-cooled cover and a horizontal bore. The internal cavity of the body and the hog is lined with refractory material. Axial feed nozzles (5 pcs.) And low pressure air pipelines (4 pcs.) Are mounted on the cover. A tangential gas burner with a channel for supplying preheated low-pressure air is installed in the upper part of the vertical housing. Below the burner in the casing wall at three levels there are made radial channels for supplying low pressure air to the cavity of the casing (1st and 2nd zones) and into the hog. Hydrocarbon raw materials and the main part of low-pressure air are axially fed into the cavity of the housing through the raw nozzles and piping of the cover, respectively. The number of nozzles used and the consumption of raw materials depend on the brand of carbon black obtained. The raw material is partially oxidized in the air stream and mixed with the combustion products formed during the combustion of natural gas in a low pressure air stream in a gas burner. When the mixture moves down, its evaporation and thermal decomposition occurs with the formation of carbon black. The dispersion and structure of carbon black are controlled by changing the amount of air supplied through the housing cover and side channels of the 1st and 2nd zones. The increase in air flow through the housing cover (along the periphery of the raw flame) contributes to a decrease in the level of dispersion and structurality. In this case, the reaction time of the formation of carbon black is increased due to the slower mixing of raw materials and air. With an increase in the amount of air supplied to the side channels, mixing processes intensify, the reaction rate increases, which leads to an increase in the specific surface and absorption of dibutyl phthalate. The resulting carbon black enters the horizontal bore, into which low pressure air is also supplied through the channel in the housing. In this case, the temperature in the hog rises, and not completely decomposed hydrocarbons are removed from the surface of the carbon black, which contributes to the achievement of a high level of light transmission of the toluene extract. At a reactor of this design receive low-dispersed carbon black grades N660, N650, N539, N550, P514. The disadvantages of the prototype are:

- low reactor efficiency due to the fact that part of the hydrocarbon feed is burned when axially introduced into the casing together with the air stream;

- the complexity of the design and insufficient reliability of the reactor associated with the use of a water-cooled cover;

- all stages of the technological process (combustion, mixing of raw materials with combustion products, evaporation of the mixture, pyrolysis) occur in the entire volume of the vertical reactor vessel. As a result, low-pressure process air is introduced into the housing distributed over the height to control the process. It leads to:

- decline in product quality due to the high likelihood of grit formation;

- increase the overall dimensions of the reactor;

- complicating the design of the reactor and its operation;

- the use of boron only to remove from the surface of carbon black is not completely decomposed hydrocarbons;

- coke formation at the transition site from the vertical casing to the hog.

The objective of the invention in terms of the device is to increase the efficiency of the reactor while maintaining the quality of the resulting low-dispersed (low-activity and semi-active) carbon black, increasing the reliability of the reactor, simplifying the design and operation of the reactor, reducing its overall dimensions.

The problem is solved due to the fact that in the reactor to obtain low-dispersed [low-activity and semi-active] carbon black of a vertical type, including a vertical cylindrical body, the inner cavity of which is lined with refractory, equipped with a lid, tangential gas burners that form a rotating flue gas stream, raw material nozzles for hydrocarbon feed and input channels into the housing of low pressure air for burning fuel and for conducting the process, and g rizontalny hog inside refractory lined and equipped with nozzles for injecting cooling water into the hog introduced features are as follows.

In the inner cavity of the vertical cylindrical casing, a local narrowing was made in the form of a nozzle with a confuser and a diffuser, the diameter of the critical section (neck) of which is 0.75-0.8 of the inner diameter of the casing, forming a combustion chamber in its upper part and a chamber evaporation. The evaporation chamber smoothly passes into a vertical cylindrical channel with a ratio of diameters of 1: (0.45 ÷ 0.5), communicating with a horizontal boron, which is a reaction chamber, with a ratio of their diameters of 1: 1.1. The cover of the vertical housing, lined with a refractory inside, forming a dome vault, is made with the vertical housing integrally and provided with an axial pipe for inspecting the internal cavity of the housing. Radial pneumomechanical or mechanical feed nozzles are uniformly installed in the nozzle neck, and the nozzle tips of the mechanical nozzles are rotated in a horizontal plane at an angle of 90-170 ° relative to the tangential velocity vector of the rotating flue gas stream. Tangential channels are made in the wall of the evaporation chamber for introducing low pressure air and swirling it in a direction opposite to the direction of rotation of the flue gas stream.

To obtain semi-active carbon black use pneumomechanical raw material nozzles, and to obtain a low-active carbon black use mechanical raw material nozzles.

The number of raw nozzles should be at least 6.

Tangential gas burners, the amount of which is determined by the productivity of the reactor, but not less than four, are placed uniformly around the circumference of the combustion chamber.

The implementation of the invention on the device

Figure 1 shows the design of the reactor to obtain low-grade grades of carbon black. The reactor contains a vertical cylindrical body 1, made with the upper cover 9 completely, and a horizontal bore (reaction chamber) 6. Housing 1 [including the cover 9] and reaction chamber 6 are lined from the inside with shaped refractory.

Inside the vertical casing 1, a local narrowing is made in the form of a nozzle 10 with a confuser and a diffuser, which divides the cavity of the casing 1 into chambers. A combustion chamber 2 is located above the narrowing 10, and an evaporation chamber 4 is located below. The diameters of chambers 2 and 4 are the same and amount to 2940 mm. The length of the combustion chamber is determined by the conditions of complete combustion of the fuel and the allowable thermal load of the dome vault of the cover 9.

Combustion chamber 2 is designed to burn fuel - natural gas in a stream of low pressure air in order to create the necessary heat reserve for the process. To this end, tangential diffusion gas burners 11 are installed uniformly around the circumference of the housing in the combustion chamber, which burn fuel and generate a heat volume in the form of a rotating flue gas stream moving axially downward inside the housing 1.

A mixing zone 3 is formed on the local narrowing section, intended for intensive mixing of hydrocarbon feedstocks with a rotating flue gas stream. To this end, in the neck (cylindrical part) of the nozzle 10, the diameter of which is 2400 mm, radial pneumomechanical or mechanical raw nozzles 12 are installed uniformly around the circumference. The nozzle tips 13 (Fig. 1 A-A) of the mechanical nozzles are rotated in a horizontal plane at an angle of 90 -170 ° relative to the tangential velocity vector of the rotating flue gas stream.

Below the local narrowing is located the evaporation chamber 4, intended for the evaporation of hydrocarbons. In the wall of the housing 1 in the lower part of the evaporation chamber 4 there are tangential channels 14 (FIG. 1 B-B) that introduce low pressure air into the evaporation chamber 4 and twist it in the opposite direction to the direction of rotation of the flue gas stream. The evaporation chamber in the lower part smoothly passes into a vertical cylindrical channel 5, the diameter of which is 1400 mm, communicating with the reaction chamber 6. Channel 5 passes into the reaction chamber 6 with a rotation of 90 ° and an extension of 1: 1.1.

A pyrolysis zone 7 is located at the initial portion of the reaction chamber 6. A cooling zone 8 is located at the final portion of the pyrolysis zone 7, in which radial water nozzles 15 are installed for introducing water into the reaction product stream (carbon-gas mixture), which evaporates in the cooling zone 8, stopping the reaction and cooling the stream to a predetermined temperature.

The reactor operates as follows.

Fuel [gas at a pressure of 1.5-2.0 kgf / cm ² ) and process air preheated in recuperative air heaters to a temperature of 450-650 ° C are introduced into the combustion chamber by 2 tangential burners 11. Gas-air mixture from burners 11 the outputs of which are located around the inner surface of the combustion chamber 2, propagates tangentially along its surface, providing the organization of combustion of the mixture in the form of a swirling stream of flame. The flue gas stream resulting from combustion, rotating with a tangential speed of 20-50 m / s, moves down with an axial speed of 0.6-1.0 m / s and reaches mixing zone 3, made in the form of a mixing nozzle 10 with a conical confuser and diffuser. Due to the presence of a conical confuser, a smooth narrowing of the flow occurs and an increase in the axial velocity of the flue gases in the nozzle neck (critical section) to 1.1-1.5 m / s while maintaining the shape of the flow. Installed in the nozzle throat 10, radial pneumomechanical or mechanical feed nozzles 12 inject hydrocarbon feed into the rotating flue gas stream, provided that the ratio of the feed rate and the tangential velocity of the flue gas in the injection zone 1: (2 ÷ 4). In order to intensify the process of crushing droplets of raw materials and mixing them with flue gases, the nozzle tips 13 of the mechanical nozzles 12 are deployed in a horizontal plane at an angle of 90-170 ° relative to the tangential velocity vector of the rotating flue gas stream. The high resulting (axial and tangential) flow velocity in the nozzle throat, as well as the introduction of raw materials at an angle, contribute to the emergence of significant shear forces that contribute to intensive crushing of the droplets of the raw material, its effective evaporation and mixing with flue gases, while preventing droplets of non-evaporated raw materials from entering the internal surface. This significantly reduces the likelihood of grit formation. Next, the resulting flow of the hydrocarbon-gas mixture through the diffuser enters the evaporation chamber 4, into the lower part of which the process air preheated to a temperature of 450-650 ° C is introduced through the tangential channels 14. The channels 14 are designed so that the air introduced tangentially swirls in the direction opposite to the direction of rotation of the flue gas stream. The amount of air introduced is set to the reactor, respectively, the performance of hydrocarbon feed and the brand of carbon black. Then, the flow of the formed hydrocarbon vapor with a speed increase of up to 9-14 m / s through the vertical channel 5 passes to the reaction chamber 6. When entering the pyrolysis zone 7 located in the initial section of the reaction chamber 6, the flow velocity is reduced to 8.5 ÷ 13 m / s due to an increase in diameter by 1.1 times. The length of the pyrolysis zone 7 is determined by the residence time of hydrocarbons in it to complete the process of formation of carbon black. For inactive carbon black, this time is 2-4 s, and for semi-active carbon, 0.8-2 s. Next, the carbon-gas mixture enters the cooling zone 8, where cooling water is injected into it with radial nozzles 15 in order to stop soot formation reactions and reduce the temperature to a level that ensures its safe use in regenerative heating devices located downstream of the technological process.

Achievable technical result

Improving the efficiency of the reactor while reducing overall dimensions and increasing the yield of low-dispersed (low-activity and semi-active) carbon black, which in its parameters meets the requirements of the international specification ASTM D1765 and GOST 7885-86.

Improving reliability, increasing the life of the reactor and the turnaround time [at least 3 years between overhauls] with the effective operation of the reactor with a hydrocarbon production rate of up to 5000 kg / h and stable quality of the products.

Claims (7)

1. A method of producing a low-dispersed (low-active and semi-active) carbon black from liquid hydrocarbon raw materials by thermo-oxidative decomposition in a vertical type reactor, including preliminary heating of liquid hydrocarbon raw materials to a temperature of 150-200 ° C, process air due to recuperative heat exchange with carbon black aerosol to temperature 450-650 ° C, mixing fuel with heated process air with a coefficient of excess air 1.2-1.3, organization of complete combustion of fuel cm B in the combustion zone at a temperature of 1540-1700 ° C to obtain a flue gas with a residual rate of active oxygen complete combustion of fuel by the number of residual air of 0.4-1.0 Nm ³ per 1 kg of hydrocarbon feedstock, mixing the hydrocarbon feedstock in the flue gas stream in the mixing zone, the evaporation of hydrocarbon raw materials, its thermo-oxidative decomposition (pyrolysis) with the formation of a carbon black aerosol, preliminary cooling by injection of chemically purified water and its subsequent cooling, characterized in that the method is carried out are installed in the reactor claimed in claim 4, in which the combustion chamber, the mixing zone and the evaporation chamber are in the vertical part of the reactor, and the pyrolysis zone and the preliminary cooling zone are in its horizontal part (reaction chamber), while the combustion of the fuel mixture is organized in cyclone-type combustion chamber with the formation of a flue gas stream rotating at a tangential velocity near the wall of 20-50 m / s, moving axially downward at a speed of 0.6-1.0 m / s and entering the mixing zone with an increase in speed to 1.1 -1.5 m / s achieved by smart Decreasing the cross section in the mixing zone, where hydrocarbons are fed into the rotating flue gas stream in several jets, provided that the ratio of the feed rate and the tangential velocity of the flue gas in the injection zone is 1: (2 ÷ 4), then the resulting hydrocarbon-gas mixture stream through the diffuser enters the evaporation chamber, into which the process air preheated to a temperature of 450-650 ° C is tangentially fed, swirling in the direction opposite to the direction of rotation of the flue gas stream, ensuring the working temperature The temperature in the evaporation chamber is 1400-1650 ° С, then the flow of the formed hydrocarbon vapor with an increase in speed to 9-14 m / s due to the increase in volume and the narrowing of the evaporation chamber passing into the vertical channel passes to the horizontal reaction chamber, where it enters with decreasing speed up to 8.5-13 m / s by increasing the diameter by 1.1 times, and where in the pyrolysis zone the temperature is set to 1240-1360 ° C and its residence time of 0.8-4 s is ensured. 2. The method according to claim 1, characterized in that to obtain a semi-active carbon black hydrocarbon feed is introduced radially. 3. The method according to claim 1, characterized in that in order to obtain a low-active carbon black, hydrocarbon feeds are introduced at an angle of 90 ... 170 ° relative to the tangential velocity vector of the rotating flue gas stream. 4. A reactor for producing low-dispersed carbon black, including a vertical cylindrical body, the inner cavity of which is lined with refractory, equipped with a lid, tangential gas burners forming a rotating flue gas stream, raw material nozzles for supplying hydrocarbon raw materials and input channels into the process air housing, and a horizontal bore lined inside with a refractory and equipped with nozzles for injecting cooling water, characterized in that in the inner cavity of the qi the local case narrowing is made in the form of a nozzle with a confuser and a diffuser, the diameter of which is 0.75-0.8 of the inner diameter of the body, forming a combustion chamber in the upper part of the cavity, and an evaporation chamber in the lower part, which smoothly passes into a vertical cylindrical channel the ratio of diameters 1: (0.45 ÷ 0.5), which communicates with the reaction chamber with a ratio of diameters of 1: 1.1, the cover of the vertical case, lined with refractory from the inside, forming a dome vault, is made integrally with the vertical case and provided with an axial A radial pneumomechanical or mechanical raw nozzle is installed uniformly around the nozzle neck to inspect the internal cavity of the housing, and the nozzle tips of the mechanical nozzles are rotated in a horizontal plane at an angle of 90 ... 170 ° relative to the tangential velocity vector of the rotating flue gas flow, and in the chamber wall Tangential channels for introducing process air and swirling it in a direction opposite to the direction of flow rotation flue gas. 5. The reactor according to claim 4, characterized in that the pneumo-mechanical nozzles are used to produce semi-active carbon black, and the mechanical nozzles are used to produce low-active carbon black. 6. The reactor according to claim 4, characterized in that the number of feed nozzles must be at least 6. 7. The reactor according to claim 4, characterized in that the tangential gas burners, the amount of which is determined by the productivity of the reactor, but not less than four, are placed uniformly around the circumference of the combustion chamber.