RU2668447C1 - Method of gasification of solid fuel and device for its implementation - Google Patents

Abstract

FIELD: technological processes.SUBSTANCE: invention can be used in the chemical and energy industries. Processing of the solid crushed fuel is carried out by gasification in a dense layer moving along the axis of a rotating inclined cylindrical reactor with a steam-water jacket. At the first stage in the upper part of the reactor, an inverted gasification process is conducted with air blasting into the upper reaction zone, where the fuel is partially oxidized and partially gasified, and the main part of it moves to the activation zone, where at a temperature above 800 °C is treated with superheated steam, which is injected from the steam-water jacket through a perforated wall. Produced activated carbon is accumulated in the buffer gas sampling zone of the reactor, and the resulting vapor-gas mixture is transported to the reaction zone of the second stage of gasification, where a direct process of gasification of the moving bed of activated carbon is implemented with counter filtration of the produced fuel gas through it, which is withdrawn from the reactor and cooled in a water evaporative heat exchanger-steam generator, where the resulting water vapor enters the steam-water jacket, and the cooled fuel gas to the consumer. Gasification reactor is additionally equipped with a device for supplying air to the upper reaction zone, as well as a vapor-gas outlet channel to the lower reaction zone of the direct gasification process. For removal of combustible fuel gas filtered through the activated carbon layer, a gas sampling channel with a water evaporative heat exchanger-steam generator is provided in the delivered and built-in design and, possibly, with a gas-air cooler of gas, as well as with a gas analyzer-converter to control the chemical composition and temperature of the produced gas.EFFECT: proposed invention makes it possible to increase the completeness of fuel processing, the quality and calorific value of fuel gas, to reduce heat losses, and to increase the compactness, economy, reliability and durability of the reactor.9 cl, 10 dwg

Description

IPC F23G 5/00 - incineration of waste or low-grade fuels,

F23G 5/027 - with a pyrolysis or gasification step

F23G 5/20 - with combustion in rotating or oscillating drums

F23G 5/46 - Heat recovery

F27B 7/20 - Methods or devices for burning only solid fuels ..., structural elements, accessories and equipment for this type of furnace

IPC C10J 3/00 - production of gases containing carbon monoxide and hydrogen, for example synthesis gas or household gas, from solid carbon-containing substances using partial oxidation processes including oxygen or steam,

C10J 3/02 -... Gasification of lump fuel in a fixed bed C10J 3/06 -... Continuous methods

C10J 3/16 - ... with the simultaneous reaction of oxygen and water with a carbon-containing material

C10J 3/20 - ... devices; setting

C10J 3/76 - ... water shirts; steam boiler shirts

The method of gasification of solid fuel and a device for its implementation

The invention relates to the field of chemical technology and power engineering based on the use of renewable energy sources and local fuels, in particular biomass and local low-grade carbon-containing raw materials, including bituminous (wood, peat, brown coal, various agricultural waste), including the disposal of municipal solid waste and industrial carbonaceous wastes, by gasification to produce combustible fuel gas containing carbon monoxide and hydrogen, for subsequent use as the power gas in vehicles and power plants.

The priority area of scientific and technological progress in the energy sector is the creation and development of effective technologies for the use of local energy resources to build a sustainable decentralized energy supply system with a concomitant solution to the increasingly urgent problem of recycling solid urban (household) waste.

Thus, the “Energy Strategy of Russia for the Period until 2030” provides for “... the development of small energy in the decentralized energy supply zone by increasing the efficiency of the use of local energy resources, including new fuels derived from various types of biomass”, which refers to low-grade fuels with high humidity (up to 85% and more), low energy density, low heat of combustion, heterogeneity of the fractional composition, but it has significant advantages compared to the spark relevant carbon-containing raw materials: renewability, almost complete absence of sulfur, as well as other chemical elements and compounds harmful to equipment and the environment, prevalence and availability. Unrefined substandard biomass (wood waste, agricultural waste, production and consumption waste, including municipal solid waste.), As well as other local fuels, primarily based on low-grade solid carbon-containing raw materials (peat and its processed products, brown coal) , together constitute fuel resources, the use of which is potentially possible in the areas (territories) of their formation, production, production and economic efficiency of consumption of which are limited ene areas (territories) of origin / RF Government Resolution of 22.022012 N 154 "On the requirements for heating circuits, the order of their development and approval" /. They are a cheap (with low, zero or negative cost) and practically not currently used source of local energy resources.

The most universal way to use these types of raw materials is their high-temperature thermochemical conversion, or gasification - burning at temperatures of 800-1300 ° C in the presence of air or oxygen and water vapor to produce fuel (aka generator) gas - a mixture of H ₂ , CO, СО ₂ , NO _x , СН ₄ / GOST R 54531-2011 Non-traditional technologies. Renewable and alternative energy sources. Terms and definitions / carried out in gasifiers (otherwise: gasification reactors, gas generators, converters), which, depending on its quality, is used in the future in a power plant (burned in a boiler unit or used as power gas, i.e., for direct energy in the engine - gas piston or gas turbine installation).

In this regard, the urgent problem is the creation of high-tech compact gasification equipment for modular autonomous small power plants for use in local small-scale energy, as sources of deep reserve electricity in territories with possible long-term emergency situations, for equipping electric vehicle charging stations in environmental and other territories, environmentally friendly waste management (as an alternative to incineration technologies).

Existing technologies and designs for gasification of solid (condensed) carbon-containing fuels are very diverse / A. Samylin, M. Yashin. Modern designs of gas generating units. - LesPromInform, No. 1, 2009, p. 78-85; Zheleznaya T.A., Geletukha G.G. Overview of modern biomass gasification technologies. - Prom. heat engineering, 2006, v. 28, No. 2, p. 61-75; Kopytov V.V. Gasification of condensed fuels: a retrospective review, current state of affairs and development prospects - M .: Infra-Engineering, 2012-504, p. 263-271 /. From an environmental point of view, their main advantage is the relatively low level of negative impact on the environment. This, first of all, is caused by the rather long (especially for gasification in a dense layer) presence of gaseous products of gasification of condensed fuels, first in the oxidation (combustion) zone at temperatures from 1000 ... 1200 ° C and higher, and then in the reduction (oxygen-free) formation zone combustible fuel gas. Under such conditions, thermal decomposition and reductive dechlorination of the most dangerous substances - dioxins, furans, polychlorobiphenyls, benzo (a) pyrenes and other polycyclic aromatic hydrocarbons occur.

The experience of long-term use of fuel (generator) gas in engines or turbines is still small. From the point of view of capital expenditures, which are higher in comparison with stations operating on fossil fuels, economically viable operation of a gasification plant in many cases is possible only when using very cheap raw materials. Interest in gasification technologies is increasingly shifting from the production of only thermal energy to the possibility of combined generation of thermal and electric energy.

Despite the notable progress made in recent years, the gas treatment system is a critical component of any gasification installation. The search continues for optimal solutions to achieve the required cleaning levels at the lowest cost. In addition, the existing gasification equipment (plants, reactors) has low energy efficiency, does not meet modern requirements for a number of operational and technical characteristics, and first of all, for compactness, simplicity and ease of maintenance, reliability, work resource, versatility in raw materials, and environmental safety, which limits its competitiveness in the global energy market.

Known technologies (schemes) for gasification / Reference. “Boiler houses and biofuel power plants. Modern technologies for producing heat and electric energy using various types of biomass. ” Ovsyanko A.D., Pechnikov S.A., St. Petersburg, Biofuel portal WOOD-PELLETS.COM. 2008 360 s. with ill .; Biomass as a source of energy. Ed. S. Soufer, O. Zaborski. - M., Mir, 1985; G.G. Tokarev. Gas generating cars. State Scientific publishing house lit., M., 1955; Kolerov L.K. Gas engine installations. M., Mashgiz 1951 / differ in the place of air supply and selection of combustible fuel gas in gasifiers and are divided into technologies and, accordingly, gasification reactors of direct, reverse (reverse) and horizontal processes.

In direct process gasifiers, the movement of solid carbon-containing fuel (hereinafter referred to as fuel) and a gaseous oxygen carrier (air, air with a high content of oxygen, oxygen) occurs in opposite directions. Gasifiers of this type are quite widespread and are, as a rule, a mine, the inner walls of which are lined with refractory material, fuel is loaded on top of this shaft, and a gaseous oxygen carrier is supplied below. The fuel layer is supported either by a grate or a layer of solid gasification residues - ash. Combustible fuel gas is discharged in the upper zone of the mine. The design of gasifiers of this type is distinguished by the execution of individual structural elements, the mutual arrangement of which, as a rule, remains unchanged. The processes of gas formation in the fuel layer in such gasifiers proceed as follows. The gaseous oxygen carrier supplied through the lower zone of the gas generator first passes through the ash zone, where it is slightly warmed up, and then enters the red-hot layer of fuel (oxidizing zone), where oxygen reacts with combustible fuel elements. The resulting combustion products, rising up and meeting with hot fuel (reduction zone), are reduced to carbon monoxide and hydrogen. With further upward movement of strongly heated reduction products, thermal decomposition (dry distillation) of the fuel (pyrolysis zone) occurs and the reduction products are enriched with decomposition products (gases, tar and water vapor). As a result of the decomposition of fuel, first semi-coke and then coke are formed, on the surface of which, when they are lowered, the combustion products are restored. When lowering even lower, coke burns. In the upper part of the gasifier, the fuel is dried by the heat of rising gases and vapors; during the selection of hot gas (with temperatures up to 300 ° C and above), gasification products are mixed with products obtained in the zones of drying and dry distillation (pyrolysis).

The direct process almost does not impose restrictions on the type and humidity of the fuel, but the resulting gas is very polluted and contains a large number of pyrolysis resins, water vapor, dust particles, etc. For its further use, deep cleaning using expensive equipment is required.

Thus, the process in the gasifier as a whole is a combination of two independent processes - dry distillation and gasification proper. In the direct gasification process, some types of fuel (the so-called bituminous fuel) produce gas with a high tar content. This makes the gas unacceptable for use as a fuel in internal combustion engines without their special purification. When this method of gasifying wood and peat, the products of dry distillation also contain acetic acid and other undesirable impurities (phenols, etc.). Gas purification from resins is fundamentally possible with the use of disintegrators, electrostatic precipitators, which complicates and increases the cost of the entire process.

In connection with the foregoing, the direct gasification process is used when using fuels with a small yield of volatile (anthracite, coke, semi-coke, charcoal).

In the reversed gasification process, fuel and a gaseous oxygen carrier move in the associated direction. Gasifiers of the reversed process, as a rule, also represent a mine, the inner walls of which are lined with refractory material, fuel is loaded on top of this mine, and in the vertical middle zone, as a rule, a gaseous oxygen carrier is supplied through the tuyeres. The fuel layer is supported by either a grate or a layer of ash. Fuel gas is discharged in the lower zone of the mine. The design of gasifiers of this type is distinguished by the execution of individual structural elements, the mutual arrangement of which, as a rule, remains unchanged. Since the evacuation of the formed gas (with a temperature of 400 ... 500 ° C) is carried out through the lower zone of the gasifier, the combustion (oxidation) zone is in the tuyere plane, a reduction zone follows this zone, above the combustion zone there is a zone of pyrogenetic decomposition of fuel due to heat of burning hot coke. Drying of the uppermost layer of fuel in such gasifiers occurs due to heat transfer from the zone of pyrogenetic decomposition of fuel. The main disadvantage is that the reversed process imposes restrictions on the humidity of the fuel (due to the absence of an active drying zone), which necessitates fuel preparation, but at the same time provides a cleaner gas with a relatively low content of pyrolysis resins and other impurities, because all dry distillation products pass through a high temperature reaction zone.

In a horizontal process, air is supplied through a lance located laterally in the lower part of the gasifier, the gas sampling lattice is located on the opposite side, and the active or reaction zone (oxidation / reduction) is concentrated in a small space between them, above which there is a dry distillation zone and above it is a zone drying fuel. This gasifier has a fairly simple design and flexibility, but cannot provide the formation of tar without gas and is not suitable for gasification of bituminous as well as multi-ash fuels.

The most promising from the point of view of increasing efficiency are combined technologies (schemes) and, accordingly, gasifiers, which allow you to take advantage of both direct and reverse gasification processes, in particular, on the basis of a two-zone gasification process / Kolerov L.K. Gas engine installations. M., Mashgiz, 1951, p. 12-15 /. The gasifier has two reaction zones (each includes an oxidation zone and a reduction zone), and in the upper part of the reactor (upper reaction zone) the fuel is gasified by the reverse process, and in the lower part (lower reaction zone), coke formed during the passage is gasified fuel through the upper zone. Gas is taken between the recovery zones, and the ash is removed during reactor operation. The process is favorable for the gasification of bituminous fuels with high ash content, however, while not sufficiently eliminating the shortcomings of the direct and inverse processes, it also has specific disadvantages associated with the high temperature of the produced gas (up to 700 ° C) and the difficulty of adjusting the air and steam blast.

Low-grade carbon-containing raw materials that are intended to be used as fuel in the present invention are typically characterized by a high content of ash and / or resins, as well as moisture. In this regard, combustible fuel gas obtained from such raw materials using existing gasification technologies (schemes) has properties that do not allow its use as a power gas, i.e. for direct energy in the engine - a gas piston or gas turbine installation, namely:

- high temperature (300 ... 700 ° C) and, accordingly, low density, which leads to a deterioration in the filling of the engine and a drop in its power;

- low volume calorific value due to the high content of ballast (nitrogen, air, moisture, carbon dioxide); so, for the most high-calorific gas produced by air blasting, less than 4000 kJ / m ^{3 of} dry gas, for the most high-calorific gas using steam-oxygen blast under pressure, about 15,000 kJ / m ³ ;

- high content of harmful impurities (ash, coal dust, soot, tarry substances, sulfur compounds, moisture), which interfere with the normal operation of the engine, cause premature wear of rubbing parts and engine failure.

In addition, for the most common hardware solutions of gasification reactors (shaft type), which are based on the movement (movement) of gasified solid lump (ground) fuel under its own weight, the stability of the flow of combustion remains an unsolved problem. Since the processed materials (especially with regard to low-grade raw materials) often have uneven gas permeability and are prone to sticking together during pyrolysis, arching, and freezing on the walls of the reactor, the pyrolysis and gasification front can spread unevenly over the reactor cross section. In the layer of the processed raw materials, “burnouts” can occur, through which the gas stream mainly flows, material collapses in the cavities formed during combustion, and almost gas-tight regions can form at the same time. As a result, the temperature distribution in the combustion zone is heterogeneous and poorly controlled, which leads to a decrease in gas quality.

Thus, for the practical use of fuel power gas, especially obtained from low-grade raw materials, it is necessary in one form or another to use a system (usually multi-stage) for its conditioning, including rather complicated and expensive equipment for cooling, drying and purifying gas (scrubbers, cyclones, electrostatic precipitators, neutralizing filters, etc.) / Kolerov L.K. Gas engine installations. M., Mashgiz 1951, with. 15-17; Directory. “Boiler houses and biofuel power plants ^. Modern technologies for producing heat and electric energy using various types of biomass. ” Ovsyanko A.D., Pechnikov S.A., St. Petersburg, Biofuel portal WOOD-PELLETS.COM. 2008, p. 248-249 /, which significantly limits the area of efficient use of gasification plants and reduces their technical, economic and operational-technical characteristics.

A number of technical solutions are known aimed at increasing the efficiency of gasification of carbon-containing, and in particular, low-grade raw materials.

Thus, the “Method for controlling the production of combustible gas and a device for producing combustible gas” is known (Eurasian patent 000184 B1, published date 12.24.1998), where to increase the purity of the gas and more fully use the carbon of the feed, the gasifying agent is fed from below to the vertical zone of the reactor through the grate and / or from above and from the side, and the gas is discharged on the side opposite the side supply of gasifying means, which helps to mix the layers of gasified raw materials, while adjusting the vertical th speed position of the reaction zone ash withdrawal, the optimum gasification temperature through the flow of the gasifying agent, the reaction efficiency by setting the band width through coordinated regulation of the gasifying means and outputting the ash. To implement the method, a grate-type step grate is provided with a drive for its repulsive movement and compaction of partially gasified fuel, and the reactor casing is provided with thermal insulation in the form of a two-layer insulating-cooling system with a perforated partition between the outer and inner layers, and the cooling agent is air used as gasifying facilities. The proposed solution is not sufficiently reliable and complicated due to the need for sorting and preparation of raw materials and the presence of moving parts in the high-temperature zone (grate), and the achieved effect is insufficient.

Also known is the “Gasifier and method for gasifying solid fuels" (Eurasian patent 009349 B1, published on December 28, 2007) based on a two-zone gasification scheme containing the stages of partial oxidation of fuel from biomass in the first oxidation zone for the production of vegetable coal, the restoration of vegetable coal in the zone reduction for the formation of ash, additional oxidation of any residue of vegetable coal in the ash in the second oxidation zone, extraction of the fuel stream produced in the above stages, through the exhaust pipe loss, moreover, in the first oxidation zone, the gas stream has the same direction as the fuel stream, and in the second oxidation zone, the gas stream has a direction opposite to the fuel stream. A fuel stream at a temperature of about 850 ° C., produced in both zones, passes through a perforated conical ring that is filled with a microporous polymer catalyst in order to crack the residual distillation liquid product before it leaves the gasifier. Thus, it is supposed to carry out gas purification, however, this leads to a complication and higher cost of the installation, and also increases operating costs

The well-known "Method for the gasification of solid carbon-containing fuel, including carbon-containing waste and a gas generator" (Eurasian patent 014373, published date 10/29/2010) involves supplying a vertically oriented carbon-containing fuel from top to bottom and a gaseous oxygen carrier flow in the direction of carbon-containing fuel movement and removal combustible gas from the lower zone of the gas generator. The flow of the gaseous oxygen carrier is fed into the vertically middle zone of the gas generator along the entire perimeter with the simultaneous formation of downward-directed streams of carbon-containing fuel and directed upward against the direction of movement of the carbon-containing fuel, while additionally the combustible gas is removed from the upper zone of the gas generator. The specified technical solution combines the advantages of the direct and reverse gasification process, but does not exclude the disadvantages of the dual-zone process.

In the well-known “Method for preparing fuel, including for burning and a device for its implementation” (patent RU 2301374, Kondra E.I. et al., Publication date 20.06.2007), fuel is fed into the reactor, it is moved towards the gaseous oxidizing agent containing oxygen, and get coke in the area of pyrolysis and coking of the fuel located in the reactor between the places of entry into the reactor of fuel and oxidizer. Coke is treated with steam generated when water is supplied to a reactor such as a tunnel furnace to cool a solid residue or target product before it is discharged from the reactor. The water gas resulting from the interaction of coke with water vapor is either taken out of the reactor to be used as a fuel gas of a heat engine, or directed towards the coke transported through the reactor to the place where the oxidizer is introduced into the reactor, and it is burned there, obtaining the fuel needed for coking, pyrolysis and drying of the fuel heat and removing generated gas from the reactor. Depending on the type of source fuel and the processing mode, the solid target product may be coke, charcoal or activated carbon. The technical solution seems to be very difficult to implement and does not imply a complete cycle of raw material processing.

The well-known “Solid fuel gasifier” (patent RU 2315083, Knyazev A.E., published on 08/10/2007) is multi-stage, while in the first stage drying, pyrolysis and partial combustion of fuel occurs, on the upper boundary of the heat spot of the second stage, all burn out of oxygen generated as a result of steam splitting, at the third stage, carbon residues are burned and absorbed.

Each stage is equipped with a device for supplying steam, located below the device for ignition and stabilization of combustion. The invention provides for the complete combustion of lump fuel without preliminary preparation, however, it is rather complicated, and the resulting fuel gas requires conditioning.

Significant advantages in the development of effective technical solutions are gasification technology according to the direct process scheme in a dense layer with a counter flow of a gasifying agent (in particular, air) and fuel, since it makes it possible to use low-calorific fuels with humidity up to 40 ... 50% with high efficiency . thermal process (up to 95%). /Directory. “Boiler houses and biofuel power plants. Modern technologies for producing heat and electric energy using various types of biomass. ” Ovsyanko A.D., Pechnikov S.A., St. Petersburg, Biofuel portal WOOD-PELLETS.COM. 2008 360 s. with ill., p. 111-151; Biomass as a source of energy. Ed. S. Soufer, O. Zaborski. - M., Mir, 1985; Kopytov V.V. Gasification of condensed fuels: a retrospective review, current state of affairs and development prospects - M .: Infra-Engineering, 2012. - 504 pp. /.

Such a solution is proposed in the "Method for processing condensed fuel and a device for its implementation. (Patent RU 2376527, Zhirnov, Zaichenko, Manelis, Polyanchik, published date 12/20/2009). This method implements a scheme for the gasification of solid organic fuels, including biomass fuel, in countercurrent gasification agent (direct gasification process), and differs in that the vapor-air gasification in a dense layer is carried out in the filtration combustion mode with super-adiabatic heating in a cylindrical inclined rotating gasifier reactor / Kislov V.M. Gasification of wood and its components in a filtration mode. Abstract of dissertation for the degree of KFMN. IPCP RAS, Chernogolovka, 2008; Zaichenko A.Yu. The effect of the motion of the solid phase on the nature of filtration combustion. Abstract of dissertation for the degree of candidate of physical and mathematical sciences Chernogolovka - 2008. IPCP RAS.

It involves loading fuel (crushed to ensure mixing and gas permeability) into a cylindrical reactor, supplying a gasifying agent containing oxygen to the reactor from the side of the reactor, where solid refined products are accumulated, loaded fuel moves along the axis of the reactor, and solid refined products are removed from the reactor, conclusion from the reactor of products of drying, pyrolysis and combustion in the form of combustible fuel gas (product gas), so that gasification is carried out by means of the fuel remains in the heating and drying zone, the pyrolysis zone, the combustion zone (oxidation / reduction reaction zone) and the cooling zone, and the gas stream is filtered through the loaded fuel layer, passing through the cooling zone, the combustion zone, the pyrolysis zone and the heating and drying zone.

In the reactor, in the zone where the temperature is maximum / exceeds 400 ° C, water is supplied in liquid form. To ensure uniform distribution over the reactor cross section of water vapor evaporated on heated solid materials of the mixture, the process is carried out in an inclined rotating reactor installed at an angle to the horizon in the range from 22 to 65 °. The temperature in the core is limited by evaporative internal cooling in conjunction with passive cooling due to endothermic reactions. The advantages of this method is the high efficiency of the process of gasification of fuels, including finely dispersed and prone to sintering, namely, stability and high efficiency gasification, the absence of unreacted fuel in the waste, low levels of harmful emissions into the atmosphere.

At the same time, the specified method has inherent disadvantages of the technological scheme of the direct process associated with a high content of tar and ballast substances in the resulting gas. Also significant disadvantages of the method are the complexity and unreliability due to the presence of additional devices in the high-temperature zone (water supply pipe; temperature sensors to control the operating parameters of gasification; seals ensuring the tightness of the reactor during rotation). With changes in the parameters of raw materials (bulk density, fractional composition, etc.), the gas permeability of the layer of processed products (ash) may be deteriorated due to sintering and unreacted fuel, which does not allow maintaining the optimal parameters of the steam-air blast and complicates the operation of the unloading device.

Also, the problem of thermal protection of the reactor structure (side wall, unloading device) has not been solved to reduce heat loss and ensure its reliability and durability. Typically, shell lining is used from the inside with insulating masonry, however, such protection is insufficient, reliability, maintainability and the service life of such structures are low, insufficient compactness, high mass and dimensional characteristics limit the use of reactors in small-sized, mobile and semi-stationary power plants designed for decentralized power supply. In addition, the presence of only one water supply point prevents the uniform distribution of steam, especially with a large reactor, which reduces the ability to control the operating parameters of gasification in order to optimize them for various types of fuels.

These shortcomings were partially eliminated in the technical solution “Method for gasification of fuel biomass and a device for its implementation” (Application for invention RU 2015156390 A, Zabegaev, Tikhomirov et al., Date of publication of the application 06/29/2017, bull. No. 19), which is the closest to the claimed invention in the aggregate of essential features.

The method involves gasification of fuel biomass in a dense layer moving along the axis of a cylindrical reactor installed at an angle to the horizon in the range from 22 to 65 ° and rotating around its axis. It includes loading into the reactor fuel biomass, which is used as solid crushed biofuel, supplying to the reactor a gasifying agent containing oxygen from the side of the reactor, where the solid products of combustion residues accumulate from the reactor, and the withdrawal of combustible fuel gas from the reactor, while gasification is carried out by consecutive stay of fuel biomass in the heating and drying zone, pyrolysis zone, active oxidation / reduction zone (reaction zone) and cooling zone, and gas flow formed by the supply of a gasifying agent containing oxygen passes successively a cooling zone, a reaction zone, a pyrolysis zone and a heating and drying zone, the final gasification product — combustible fuel gas — being filtered through a layer of loaded fuel biomass, and the water being supplied to the reactor in the form of steam, the formation of which occurs in the evaporation cavities of a steam-water jacket (belt of a steam-water curtain), directly adjacent to the inner wall of the working chamber of the reactor, due to pilaf stream from the reaction zone, wherein the injection of superheated steam is carried into the reaction zone through the perforated inner wall of the working chamber of the reactor, providing heat protection of the working chamber of the reactor inner wall with the localization of the high-temperature zone in the center of the reaction zone.

However, the proposed technical solutions do not eliminate the shortcomings of the technological scheme of the direct process associated with the high content of tar and ballast substances in the resulting gas, as well as its high temperature.

The present invention is aimed at solving the technical problems of increasing the efficiency of gasification of carbon-containing, and primarily low-grade raw materials, ensuring the quality of power gas for direct use in engine systems, and above all, high calorific value and low levels of harmful impurities, as well as reduce heat loss in the gasifier reactor and ensuring its compactness, as well as efficiency, reliability and durability.

To solve the tasks, a method for gasification of solid fuel in a dense layer moving along the axis of a cylindrical reactor, installed at an angle to the horizon in the range from 22 to 65 ° and rotating around its axis, including loading prepared - ground, compacted - solid fuel into the reactor, is proposed, which use solid biofuel (GOST 33104-2014. Solid biofuel. Terms and definitions /, obtained directly or through intermediate steps from biomass (primary biomass and solid waste processing methods, the organic part of solid urban (household) waste), and / or solid low-grade fossil carbon-containing raw materials (peat, brown coals), the gasification agent is supplied to the reactor - air, from the side of the reactor where the accumulation of solid gasification residues takes place, the loaded solid fuel along the axis of the reactor, the withdrawal of solid gasification residues from the reactor, the withdrawal of combustible fuel gas from the reactor, water supply to the reactor. Gasification is carried out in a reactor equipped with a steam jacket integrated in the space inside the double side wall, consisting of an outer wall - a casing and an inner wall of the working chamber of the reactor; water is supplied to the reactor by self-injection of water vapor superheated by the heat flux from the working chamber of the reactor, from the steam-water jacket through the perforated inner wall of the working chamber of the reactor, and the resulting combustible fuel gas is filtered through a layer of loaded solid fuel.

Moreover, in contrast to the known method, the gasification process is carried out according to a two-stage scheme. At the first stage, in the upper part of the reactor, including the heating and drying zone, the pyrolysis (coking) zone, and the additional (upper) reaction zone, a reversed partial gasification process is implemented, which involves supplying air (air blast) to the upper reaction zone.

The solid fuel that has moved there in the form of coke is partially oxidized (burned) and partially gasified, and its main part moves further to the activation zone, where at temperatures above 800 ° C it is treated with water vapor that is superheated due to the heat flux from the working chamber of the reactor and supplied by self-injection from a steam-water jacket through the perforated wall of the working chamber of the reactor. The resulting activated carbon is accumulated in the buffer gas sampling zone below, and the resulting vapor-gas mixture of pyrolysis gas residues and unreacted water vapor is transported to the lower reaction zone of the second gasification stage, where a direct gasification process of the activated carbon layer moving from the buffer gas sampling zone with counter filtration is implemented through it, the resulting combustible fuel gas, which is then removed from the reactor and supplied to the consumer.

By means of a sequential two-stage scheme with intermediate processing of gasified solid fuel with superheated steam, the completeness of fuel processing and an increase in the calorific value of the resulting combustible fuel power gas are ensured, and an increase in its purity is achieved, firstly, by decomposition of the resins contained in the pyrolysis gases and by the complete reaction of water vapor with carbon and secondly, by filtering combustible fuel gas through a layer of activated carbon accumulated in the buffer gas sampling zone. In this case, it is potentially possible to almost completely eliminate the moisture content in the resulting fuel gas, including both the hygroscopic moisture of the feedstock and the reaction (chemical) moisture, as well as moisture additionally introduced in the gasification process at the stage of coal activation. Reducing heat loss and lowering the temperature of the fuel gas when it is supplied to the consumer is achieved by regenerative water evaporative cooling, which is carried out by constructing a gasifier, including a reactor with a gas sampling channel and a water evaporative heat exchanger-steam generator (in the external or built-in version), into which it is supplied under pressure from the outside water, and the water vapor obtained as a result of heat exchange (saturated or irrigated) is supplied to the steam-water jacket built into the wall of the reactor, where n is overheated due to heat flow from the reactor and enters the working chamber by a perforated wall through samoinzhektsii a wall region of the working chamber in the activation zone, and the cooled combustible fuel gas is supplied to the consumer.

The cooling efficiency of combustible fuel gas can be improved by additional cooling with air, which is then supplied in the required volume by air blast to the reaction zones of the reactor.

A high degree of purification of the resulting combustible fuel gas can be additionally supported by controlling the chemical composition (in particular, the level of moisture, carbon dioxide) and the temperature of the combustible fuel gas with adjustment of the absolute and / or relative productivity of gas blowing of the vapor-gas duct, gasifier supply devices - air to the lower and upper parts of the reactor, as well as blowers of the gas-air heat exchanger.

The invention is illustrated in FIG. 1-10.

In FIG. 1 shows a general diagram of a device — a solid fuel gasifier in a dense layer in an inclined rotating reactor of a two-stage (or two-zone) type.

In FIG. 2 shows a section AA according to FIG. one.

In FIG. 3 shows a section bB according to FIG. one.

In FIG. 4 shows a General view of the gasifier with the reactor in the working (inclined) position (at an angle α to the horizontal).

In FIG. Figure 5 shows a general diagram of a device for a particular case of constructing a gasifier with a gas analyzer-converter and a control bus for gas blowing of a steam-gas outlet channel, as well as with a steam-water jacket of a reactor with a configuration that makes it possible to isolate the activation zone.

In FIG. Figure 6 shows a general diagram of a device for a special case of constructing a reactor with a water-based evaporative heat exchanger-steam generator in built-in design, as well as with a gas analyzer and control buses for gas blowing of a steam-gas outlet channel, blowers of the upper and lower devices for supplying a gasifying agent - air and a gas-air blower heat exchanger.

In FIG. 7 shows a section AA according to FIG. 6.

In FIG. 8 shows a section bB according to FIG. 6.

In FIG. 9 shows a detail fragment B according to FIG. 6.

In FIG. 10 shows a section GG according to Fig. 6.

The method of gasification of solid fuel is carried out by means of a gasifier device (Fig. 1-10), which operates as follows.

The initial solid fuel “F” (hereinafter referred to as the fuel) is biofuel obtained directly or through intermediate stages from biomass (primary biomass and solid waste from its processing, the organic part of solid urban (household) waste), and / or solid low-grade fossil carbon-containing raw materials ( peat, brown coals), if necessary previously prepared to ensure gas permeability and flowability (mixing), in particular, crushed (for lumpy raw materials) or compacted (for raw materials with a low bulk density of silt finely dispersed materials) and, possibly, with the addition of solid non-combustible material, is loaded through a loading device 3, which includes a hopper with a lock chamber and a vertical cylinder, into the working chamber of the reactor, where the level of loaded fuel is kept constant, since the reactor rotates from the vertical cylinder (Fig. 1).

The fuel “F” in the reactor in the form of a dense layer, stirred during rotation of the reactor around its axis, passes sequentially through the heating and drying zone 4, the pyrolysis (coking) zone 5 to the upper reaction zone (oxidation / reduction zone) 6, where through the feed device gasification agent in the upper part of the reactor 22 through the upper air blast channel 21 (for example, an annular shape, partitioned to ensure uniform distribution of air supply using longitudinal stiffeners 25) air "A" is supplied. In the upper reaction zone 6, reactions of incomplete oxidation of the fuel occur with a limited supply of oxygen in the composition of the air blast. During gasification, reactions occur both with the release of heat and with its absorption, therefore, to maintain the process, the condition of autothermality must be ensured, in which the total thermal effect of all reactions will be zero.

Upon receipt of air gas, when air enters the gas generator as blast, the oxidation and reduction reactions occur according to the following scheme:

C + O ₂ → CO ₂ +97650 kcal

2C + O ₂ → 2CO + 58860 kcal

2CO + O ₂ → 2CO ₂ +136440 kcal

CO ₂ + C → 2CO-38790 kcal

The high temperatures achieved in this case are favorable for the completion of carbon dioxide reduction reactions, however, they can exceed the softening temperature and even the liquid-melting state of the ash of a number of solid fuels (the melting point of biomass is usually not lower than 1150 ° C / Reference. "Boilers and power plants using biofuels. Modern technologies for producing thermal and electric energy using various types of biomass. ”Ovsyanko AD, Pechnikov SA, St. Petersburg, Biofuel portal WOOD-PELLETS.COM. 2008, p. 32 /). This leads to disruption of the normal operation of the reactor, since large fused pieces of slag are formed, which impede air access and the gas generation process, the apparatus itself overheats, its performance decreases, its efficiency decreases, and the gas quality decreases. To reduce the temperature of the process, water vapors are introduced into the reactor together with air blasting (mixed generation process - steam-air blasting). Steam blasting produces water gas. Water vapor passing through a layer of hot coke in the reduction zone enters into chemical interaction with carbon by the reactions:

C + H ₂ O = CO + H ₂ -28380 kcal; С + 2H ₂ O = CO ₂ + 2Н ₂ -17970 kcal, i.e. both reactions are endothermic, with heat absorption, which leads to a local decrease in temperature. Water gas has a higher calorific value than air gas, but the process efficiency is low.

In the upper reaction zone 6, due to the partial oxidation of carbon fuel, a temperature of 900 ... 1100 ° C is achieved, which is necessary, firstly, for the preparation of fuel in the heating and drying zone 4 and the pyrolysis (coking) zone 5 and, secondly, for reactions partial air gasification of fuel and obtaining a layer of hot coke in the activation zone 7, which is located below the upper reaction zone 6, being essentially its continuation.

Water "W" in the steam-water jacket 13, built into the space inside the double side wall, consisting of the outer wall - the casing 1 and the inner wall of the working chamber of the reactor 2, is fed through a water evaporative heat exchanger-steam generator 24, which enters from the outside under pressure through the inlet pipe 19 with check valve. Water vapor, saturated or watered, resulting from heat exchange with hot fuel gas “G” leaving the reactor through the outlet of the gas sampling channel 20, enters the steam-water jacket 13, where it overheats under the influence of heat flux (radiation) from the working chamber of the reactor, namely the upper reaction zone 6 of the reversed gasification process (at the first gasification step) and from the lower reaction zone 9 of the direct gasification process (at the second gasification step).

As a result of heating, the pressure in the steam-water jacket 13 increases, the steam is injected through the perforated along the length of the activation zone 7 section 17 of the inner wall of the working chamber of the reactor, forming there a wall heat-insulating layer in a state superheated due to pressure reduction and entering into endothermic reactions with carbon of hot fuel / coke, as a result of which a "water" combustible gas is formed and the temperature in the parietal layer is reduced (limited) during fuel mixing and distribution eniya vapor at reactor rotates. High temperature in the reaction zone is a prerequisite for ensuring high gas quality; almost complete reduction of CO ₂ in CO is ensured at temperatures of at least 950 ... 1000 ° C / G.G. Tokarev. Gas generating cars. Gos. scientific and technical publishing house lit., M., 1955, p. 23, 31 /.

At high temperatures of hot coke (above 800 ... 850 ° C) endothermic reduction reactions occur with the formation of water gas. Such treatment with superheated steam makes it possible to obtain activated carbon from coke with the necessary properties for its further use in the process as an adsorbent / Kinle X., Bader E. Active carbons and their industrial applications. - M .: Chemistry, 1984. - 216 p. /. In this case, the activated carbon layer is accumulated at a corresponding temperature decrease in the buffer gas sampling zone of the reactor below 8. The resulting gas-vapor mixture of combustible fuel gas, residues of undecomposed pyrolysis gases and unreacted water vapor are transported through the gas-vapor outlet channel, which includes the outlet of the vapor-gas mixture 14, gas pipeline with a gas blower 16 and a pipe for supplying / introducing a gas-vapor mixture 15 into the lower reaction zone 9 of the second gasification stage, where direct the gasification process of the activated carbon layer moving from the buffer gas sampling zone 8, for which air blasting is carried out using the supply of a gasifying agent - air "A" to the lower part of the reactor 12 through the cooling zone 10. There is an accumulation of solid gasification residues - ash "R", which, as the reactor rotates, pours out through the openings of the unloading device 11 into the ash bin 18. The ratio of the openings of the openings, the rotation speed of the reactor, and the flow rate of the oxidizer (air) supplied to the reactor, It provides an ash discharge rate at which the position of the reaction zone 9 in the reactor remains constant. Air “A” is supplied to the lower part of the reactor along its axis (central blast), for example, by means of a fan (blower), and the gas flow generated in this case passes sequentially to cooling zone 10, lower reaction zone 9 and further in the form of the resulting combustible fuel gas “ G "is filtered through a layer of activated carbon moving towards it in the buffer gas sampling zone 8 and then removed from the upper part of the buffer gas sampling zone 8 of the reactor through the nozzle of the gas sampling channel 20. In the second stage of gasification, almost complete decomposition of tar residues, completion of gas carbonization reactions of fuel with the formation of mixed combustible fuel gas, including water vapor and carbon reactions, as well as purification of the resulting fuel gas from impurities (ash particles, unreacted fuel carbon, soot, possible traces of resins) for due to adsorption in the activated carbon layer in the buffer gas sampling zone 8. A high degree of processing and purification of gas "G" is provided due to the length of the gas buffer zone 8, as well as a high reaction ability of fuel - activated carbon (based on the initial predominantly vegetable, including wood raw materials), its gas permeability and flowability (mixing). With the release of steam, a pressure drop occurs in the steam-water jacket 13 and steam enters into it from the water evaporative heat exchanger-steam generator 24, in which the selected combustible fuel gas "G", the temperature of which at the outlet of the reactor can reach 700 ° C and above, is cooled to supply to the consumer as power gas.

For the effective separation of gas flows in the reactor, both structural solutions (separation ring 23 on the inner surface of the working chamber wall between the activation zone 7 and the buffer gas extraction zone 8) and the regulation of operating parameters (intensity and / or ratio of air blast intensities in the upper and lower parts of the reactor, gas blowing capacity of the pipeline 16).

To improve the reliability of differentiating gas flows in the working chamber of the reactor — the vapor-gas mixture discharged in the first stage of gasification and the combustible fuel gas obtained in the second stage of gasification, the design of the steam-water jacket 13 can be different, in the particular case of execution (Fig. 5) steam-water shirt 13 may have extensions inside the working chamber, structurally distinguishing the activation zone 7 from the adjacent upper reaction zone 6 above and the buffer gas sampling zone 8 below and having a vertical section SRI trapezoidal or other similar configuration and locally narrowing chamber cross-section; while the internal, including inclined, wall sections of such a structure inside the activation zone 7 can be further perforated (perforated sections 17) for passage of superheated steam from the steam-water jacket 13 into the activation zone 7 of the working chamber of the reactor.

In addition, an increase in the reliability of separation of gas flows can be achieved by monitoring the current parameters - temperature and chemical composition of combustible fuel gas before supplying it to the consumer, taking into account that exceeding the calculated levels of gas temperature and / or the content of impurities (moisture, resins) in it due to the possible undesirable entry of a vapor-gas mixture into the buffer gas sampling zone. The specified control can be implemented by installing a gas analyzer-converter 37 in the gas sampling channel before supplying combustible fuel gas to the consumer, while the gas analyzer-converter 37 can be connected by control buses 38 with gas blowing of the vapor-gas channel 16 to adjust its performance.

To increase the compactness of the device and ensure its thermal protection, as well as the efficiency of the activation process, a technical solution of the reactor is proposed with a water vaporizing heat exchanger-steam generator integrated in the steam-water jacket (Fig. 6-10).

Moreover, the steam-water shirt 36 is an annular water tank "W", which is supplied externally under pressure via a pipe 19 with a non-return valve, with a water evaporative heat exchanger-steam generator 35 and a superheater 33.

The water evaporative heat exchanger-steam generator 35 may be a bundle of heat exchange tubes inside an annular water tank through which the produced combustible fuel gas “G” passes from the buffer gas sampling zone 8 through the internal gas exhaust channels 26 and the annular gas collection channel 39 through the heat exchange gas pipes of the steam generator 35, where it transfers heat to water, into the gas collection chamber 27 and is then removed from the reactor through the upper pipe of the gas sampling channel 34. At the same time, it is cooled to intensify the process I combustible fuel gas reactor inner wall of the working chamber 2 preferably has a ribbed structure and an upper air blow passage is provided in the form of tubes 28 arranged inside the gas collecting space 27.

Watered steam generated in the upper part of the steam-water jacket 36 enters through an overpressure check valve 29 into a superheater 33, which consists of cavities 30 formed by radial walls 31 formed by radial walls 31 in the annular space between the cylindrical partition wall 32 and the perforated section 17 of the inner wall of the working chamber of the reactor, which in turn form a cellular (cellular) structure adjacent to the perforated sections 17 of the inner wall, providing conductive samoinzhektsiyu superheated steam from the cavities (cells) 30, a superheater 33 in the wall region activation zone 7 of the working chamber of the reactor.

As a result of the heat flow from the working chamber of the reactor, increasing pressure in each individual evaporation cell 30 forces the superheated steam to flow through the perforated section 17 of the inner wall of the working chamber into the core 7.

The supply (injection) of water vapor in the chamber 2 of the reactor is automatically controlled thermally / G.G. Tokarev. Gas generating cars. Gos. scientific - those. publishing house lit., M., 1955, p. 37 /, when the amount of steam generated in each individual cell 30 and entering from it into the activation zone 7 is directly dependent on the intensity and degree of heating (temperature) of this cell.

With the release of steam, a pressure drop occurs in the cells 30 and water-vapor is again supplied to them through the overpressure check valves 29. The flow of water from the outside through the pipe 19 can be controlled (in particular, limited) by a predetermined weight ratio of water and the fuel biomass loaded into the reactor, corresponding to the desired gasification mode (composition of the resulting fuel gas).

Possible deposits (soot) on the inner surface of the perforated section 17 in the activation zone 7 of the reactor can drown out the perforation in individual cells 30, however, a local temperature increase accelerates the gasification process, eliminating deposits, and a temporary increase in steam pressure in these cells contributes to its passage into the chamber.

For additional cooling of the fuel gas, the use of a gas-air heat exchanger 40 is provided, while the exhaust (heated) air “A” in the required volume can be used as air blast in the gasifier supply device - air to the upper 22 and lower 12 of the reactor, and the excess - for drying the feedstock.

To increase the reliability of separation of gas flows, the gas analyzer-converter 37 can be connected with control buses 38 not only with gas blowing of the vapor-gas removal channel 16, but also with devices for supplying a gasifying agent - air to the lower 12 and upper 22 of the reactor, as well as with a gas-air heat exchanger blower (gas cooler) 40 to adjust their productivity / work productivity ratio.

To simplify the design of the device, in particular, to reduce the requirements for seals, you can use the pendulum mode of rotation of the reactor with a change in the direction of rotation of the reactor to the opposite after its rotation by a certain angle (for example, 180 °).

Based on reference data / see source indicated above: Reference book “Boiler houses and biofuel power plants ..., p. 110 / for a rough assessment of the effectiveness of the proposed technical solutions we will accept the following initial data:

1) an approximate composition of the resulting fuel gas during steam-air blasting,% by volume: СО-28, H ₂ -16, СО ₂ -7, N ₂ -46, СН ₄ -3;

2) gas output, m ³ / kg of raw materials: 1.87-2.35

Thermophysical parameters:

- specific heat of water C _w , kJ / kgK ........... 4.19 (std. conv.);

- specific heat of vaporization L _γ kJ / kg „……… 2 250;

- average (in the temperature range of 100 ... 700 ° C) specific heat of gases With _p , kcal / kg deg:

СО-0.27; H ₂ -3.5; CO ₂ -0.24; N ₂ -0.26; CN ₄ -0.80;

- specific weight g of gases (at 700 ° C), kg / m ³ :

CO-0.35; H ₂ -0.025; CO ₂ -0.56; N ₂ -0.35; CH ₄ -0.22;

Thus, it is possible to determine the parameters of the resulting fuel gas:

- average specific heat capacity C _p = 0.79 kcal / kg deg;

- specific gravity (at 700 ° C) g = 0.31 kg / m ³ .

In this case, the gas yield by weight will be ~ 0.6-0.7 kg per 1 kg of feedstock; to cool the indicated amount of gas to 100 ° С, a removal of 284-332 kcal, or 1.2-1.4 MJ of heat, will be required.

Heating the water entering the evaporative heat exchanger from 20 ° С to 100 ° С (Δt = 80 °) and its evaporation requires (C _w Δt + L _γ ) m (kJ) heat, where m is the mass of water (kg), from here it can be determined the mass of water required for cooling the gas, which will be ~ 0.46-0.54 kg per 1 kg of feedstock.

The optimal (by the criterion of the maximum calorific value of the generated gas) weight ratio of water and fuel K _w in the real gasification process depends on the type of raw material. So, for woody biomass K _w = 0.4 ... 0.5 / G.G. Tokarev. Gas generating cars. Gos. scientific - those. publishing house lit., M., 1955, p. 35-38 /, which practically corresponds to the obtained values for the proposed technical solution. The real heat transfer process involves the presence of heat loss, i.e. the amount of steam generated will be slightly less, which is fully compensated, firstly, by the moisture content in the feedstock - solid fuel “F” (up to 10 ... 20%) and, secondly, by supplying water with a drop of liquid along with steam state (waterlogged steam).

Claims (9)

1. The method of gasification of solid fuel in a dense layer moving along the axis of a cylindrical reactor installed at an angle to the horizon in the range from 22 to 65 ° and rotating around its axis, including loading into the reactor a pre-prepared - ground, compacted - solid fuel, as which uses solid biofuel and / or solid low-grade fossil carbon-containing raw materials - peat or brown coals, the supply of gasification agent - air - to the reactor from the side of the reactor where accumulation occurs solid gasification residues, moving the loaded solid fuel along the axis of the reactor, removing solid gasification residues from the reactor, withdrawing combustible fuel gas from the reactor, supplying water to the reactor, while gasification is carried out in a reactor equipped with a steam jacket, water is supplied to the reactor by injection of water steam, superheated due to the heat flow from the working chamber of the reactor, from the steam-water jacket through the perforated inner wall of the working chamber of the reactor, and the resulting combustible fuel the gas is filtered through a layer of loaded solid fuel, characterized in that the gasification process is carried out according to a two-stage scheme, where in the first stage in the upper part of the reactor, which includes a heating and drying zone, a pyrolysis zone and an additional reaction zone, an inverse partial gasification process is implemented, which includes the supply of gasification agent - air - directly to the upper reaction zone, where the solid fuel that has moved there in the form of coke is partially oxidized and partially gasified, and its main part The further moves to the activation zone, where it is treated with superheated steam from a steam-water jacket at temperatures above 800 ° C, and activated carbon obtained from coke is accumulated in the buffer gas sampling zone of the working chamber of the reactor, and the resulting vapor-gas mixture is removed from the activation zone and transported to the lower reaction zone at the second stage of gasification, where a direct gasification process of the activated carbon layer moving from the buffer gas sampling zone with counter filtration through its combustible fuel gas produced, which is withdrawn from the reactor and prior to feeding the consumer is cooled in the water-evaporative heat exchanger steam generator, which is fed under pressure from outside the water produced by heat exchange steam supplied in the steam jacket of the reactor and the cooled fuel gas flammable - consumer. 2. The method of gasification of solid fuel under item 1, characterized in that the combustible fuel gas before being supplied to the consumer is additionally cooled with air, which is then supplied in the required volume by air blasting to the upper reaction zone in the first gasification stage and through the cooling zone to the lower reaction zone at the second stage of gasification. 3. The method of gasification of solid fuel according to claim 2, characterized in that before supplying the consumer, the chemical composition of the combustible fuel gas is controlled, for example, the level of ballast substances — moisture and / or carbon dioxide, as well as its temperature and taking into account the current values of the controlled parameters, as well as their ratios, regulate the intensity of removal of the vapor-gas mixture, the rate of supply of gasification agent-air to the reactor, and the rate of air cooling of the combustible fuel gas. 4. The method of gasification of solid fuel according to claim 1, characterized in that air with a high oxygen content or oxygen is used as a gasification agent. 5. A device for the gasification of solid fuel in the form of pre-prepared - crushed, compacted - solid biofuel and / or solid low-grade fossil carbon-containing raw materials, which are used as peat or brown coals, in a dense layer, including a loading device installed at an angle to the horizontal in in the range from 22 to 65 °, a cylindrical reactor made with the possibility of rotation around its axis and equipped with a steam jacket integrated in the space inside the double side wall of the reactor ora, consisting of the outer wall - the casing - and the inner wall of the working chamber with a perforated section to ensure the passage of steam from the steam-water jacket into the working chamber of the reactor, a discharge device, a device for supplying a gasifying agent - air - to the lower part of the reactor, a drive for rotating the reactor, seals, ensuring the tightness of the reactor during rotation, characterized in that the reactor is additionally equipped with a device for supplying a gasifying agent - air - to the upper part of the reactor through the upper blow channel al, having, for example, an annular shape, into the upper reaction zone of the inverted gasification process of the first stage of gasification of solid fuel moving from the loading device inside the working chamber of the reactor, while the perforated portion of the inner wall of the working chamber is located along the length of the reactor activation zone, adjacent to the bottom from the top the reaction zone and designed to produce activated carbon from coke by treatment with superheated steam, and the working chamber in the activation zone has an exit to the vapor gas a discharge channel formed by a vapor-gas mixture outlet pipe, a gas pipeline with a high-temperature gas blower and a gas-vapor mixture input pipe, for transporting the gas-vapor mixture from the activation zone to the lower reaction zone of the direct gasification process, as well as the outlet to the gas sampling channel from the upper part of the gas sampling buffer zone in which activated carbon moving from the activation zone to activate from the reactor combustible fuel gas filtered from the lower reaction zone through the layer is activated th coal, and feed it to the user with its cooling in the water-evaporative heat exchanger, the steam generator also having an input for externally supplying pressurized cooling water and an outlet for supplying steam generated in the steam jacket of the reactor. 6. The device for gasification of solid fuel according to claim 5, characterized in that the steam-water jacket has extensions inside the working chamber, delimiting the activation zone from the upper reaction zone adjacent to it from above and the gas sampling zone from below, having a trapezoidal configuration in vertical section and locally narrowing the cross-section of the chamber for separating gas flows - the exhaust gas-vapor mixture and the resulting combustible fuel gas. 7. The device for gasification of solid fuel according to claim 5, characterized in that the steam-water jacket structurally includes a built-in water evaporative heat exchanger-steam generator and a superheater, while the gas sampling channel for outputting combustible fuel gas from the reactor is formed by an annular gas collection channel connected by passage openings with a buffer gas sampling zone of the working chamber of the reactor and heat-exchange gas tubes of a water evaporative heat exchanger-steam generator with an annular gas collection polo a thaw in the upper part of the reactor, which is equipped with an upper nozzle of the gas sampling channel for supplying fuel gas to the consumer, the upper blast channel for additional air inlet may have a tubular shape, and the inner wall of the working chamber of the reactor may have a ribbed structure to intensify the process of heat transfer from combustible fuel gas to supplied air and to solid fuel moving inside the working chamber in the heating and drying zone and in the pyrolysis zone, and the superheater consists of a compound connected with a water evaporative heat exchanger-steam generator through the check valves of the overpressure of the cavities forming a cellular, in particular honeycomb, structure on the wall of the working chamber, which is perforated to provide injection of superheated steam from the superheater cells into the wall region of the activation zone of the working chamber of the reactor. 8. Device for gasification of solid fuel according to paragraphs. 5-7, characterized in that the device additionally includes a gas-air heat exchanger with a blower for cooling the combustible fuel gas before supplying it to the consumer, while the outlet of the gas-air heat exchanger for exhaust air is connected to the inputs of the air supply devices to the upper and lower parts of the reactor, and to the drying channel of the feedstock. 9. Device for gasification of solid fuel according to paragraphs. 5, 6, characterized in that the device further includes a gas analyzer-converter for monitoring the chemical composition, in particular the level of moisture content, carbon dioxide, and the temperature of the combustible fuel gas after the water evaporative heat exchanger-steam generator before being supplied to the consumer, while the gas analyzer the converter can be connected by control buses with gas blowing of the steam-gas outlet channel, with devices for supplying a gasifying agent-air to the lower and upper parts of the reactor, as well as with uhoduvkoy-gas heat exchanger to adjust their absolute and / or relative performance.

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