SI25771A - Device for the gasification of solid materials with carbon content, with emphasized concentration of tar and their catalytic conversion into carbon monoxide and hydrogen - Google Patents

Abstract

The present invention discloses a device for gasification of carbon materials with a high concentration of tars and their catalytic conversion into carbon monoxide and hydrogen, containing a mixer (1) of gasification material containing dosing systems (2, 3, 4, 5), first conveyor system (6), second conveyor system (50), carburetor (8) surrounded by a first heat exchanger (28), a catalytic reactor comprising a mixing part (16), feed systems (17, 18, 19), distributor (20), catalyst (21), flame arrestor (22), ignition chamber (23), ignition elements (24) and catalyst core (25), which is made of a porous linear ceramic support and contains a plurality of parallel honeycomb channels , a second heat exchanger (30), a third heat exchanger (33) and a dehumidifier (36). The device allows the use of low-quality or more complex materials with high moisture and / or dust contents by allowing the formation of significantly higher tar contents in the product gas, which use the senate in the catalytic reactor for autothermal catalytic conversion of tars without increasing inert components in the resulting gas. N2 and CO2), while a higher tar concentration linearly increases the H2 / CO ratio in the synthesis gas.

Description

Device for gasification of solid materials with carbon content, with emphasized concentration of tars and their catalytic conversion into carbon monoxide and hydrogen

Field of the invention:

The subject of the invention is a device for gasification of carbon-containing materials for the production of pure synthesis gas.

Description of the technical problem

The technical problem solved by the present invention is to provide a gasification device for a wide range of solid materials with carbon content, which produces a product gas with a high concentration of tars and can use materials with a high content of volatile hydrocarbons (such as biomass of all kinds, biowaste , plastics, rubber, mixed municipal waste and the like), as well as low content of volatile hydrocarbons (such as coal or coal), these gasification materials need not be specially prepared in terms of dust and moisture removal or homogenized, and which may also contain materials with components S and Cl.

Another technical problem solved by the present invention is to provide a device for converting high concentrations of tars in the product gas, which can also contain solid dust particles and also tars with high molecular weights, in CO and H ₂ or in synthetic gas, by catalytic reaction. partial oxidation, which takes place at an increased concentration of tars in the product gas, which serve as a reactant in the reaction.

State of the art

Carbon gasification plants for the production of synthetic gas are well known, developed and in regular use and can be divided into:

- carburetors with a stable layer of material (Fixed bed). There are two subgroups of these: a) downdraft, in which the gasification material is dosed from the top or side of the carburetor, and the gas is discharged at the flow of the material, and b) updraft, where the material is dosed from above, from the side or from below, and the gas is discharged from the carburetor above.

~ Flow bed gasifiers, where there is no pronounced direction of air and fuel flow during intensive mixing and heat transfer in the bed. Subgroups of this technology are: a) bubble layer gasifiers, where air is supplied at a speed of about 1 m / s, and part of the gasification reactions takes place entirely in a free layer above the layer of inert material, and b) circular gasifier, where the velocities air movements higher (> 3 m / s), and most gasification reactions take place inside the suspended layer, the inert material from the product gas is filtered and returned to the base layer.

State-of-the-art fuel-flow countercurrent gasifiers are described in U.S. Pat. No. 835,847, U.S. Pat. No. 4,971,599 and U.S. Pat. No. 5,138,957. In the mentioned cases, these are carburetors where the fuel is fed through the middle of the grate from below. The grille is a fixed plate with openings for air blowing and ash removal. The gasification process takes place along the entire column of material formed in the carburetor, namely the drying zone in the upper layer, followed by the pyrolysis zone and the reduction zone, and below, just above the grate, there is an oxidation zone. The product gas formed in the pile of flammable material is discharged through an opening in the upper part of the carburetor. Such carburetors allow the use of a wide range of gasification materials that do not require special preparation and may contain dust or may be in the form of sawdust and with a high moisture content. The characteristic of the described type of gasifiers is that the product gas contains high concentrations of tars, so they are mostly used as pre-combustion boilers, where the product gas burns and uses only thermal energy, as well as the possibility of using inferior fuels unsuitable for combustion directly in the boiler. Carburetors of this type are robust and the process cannot be precisely controlled, so they are very rarely used to produce synthesis gas.

U.S. Patent 2008/0196308 discloses a technological solution for a double-jacket carburetor that acts as a regenerative gasifier tank heater. It produces high-energy synthesis gas with a low concentration of tars, which are still too high for further gas use. Due to the heating of the gasification vessel, more pyrolysis takes place in the process, causing a significant part of the carbon to remain unbound in the form of charcoal in the ash as an unwanted by-product.

Tar conversion

If the purpose of gasification is the production of pure synthetic gas from solid materials for gasification, the removal of tars is solved by primary or secondary measures. The primary measures are measures within the carburetor, namely the appropriate construction or type of carburetor and / or properly prepared fuel. However, existing types of carburetors are not sufficient to produce perfectly pure synthesis gas. For this reason, secondary procedures (behind the carburetor) with additional procedures take care of the purification of the product gas. The seconds measures can be divided into physical tar removal (filtration, washing with water) and tar conversion (breaking, cracking, reforming) (thermal or catalytic), which represents a significant advantage over the physical removal of tars. Catalytic processes for the conversion of tars or long hydrocarbons into shorter compounds or CO and H2 are a well-established process in the petrochemical industry. Numerous studies of the use of catalysts are underway in the field of gasification of solid materials. Basically, a catalytic reaction of partial oxidation and / or vapor conversion of tars is used. Catalytic reactions take place at a certain high temperature and use an internal or external heat source to maintain the operating temperature. The advantage of catalytic conversion of tars compared to thermal conversion is the reaction rate and thus lower consumption of external energy sources.

The technical problem with the investigated catalytic conversion systems with partial oxidation is in the use of product gas with very low tar concentrations. If the product gas contains little tar, complete oxidation of part of the already formed synthesis gas is used to maintain the operating temperature of the catalyst, thus increasing the content of inert components (eg CO2 and N2), thereby reducing its calorific value and efficiency of the whole system. As a result, the energy balance of the system is significantly better if the product gas contains the highest possible concentration of tars, which are themselves a high-calorie fuel. The use of a gas with a higher tar concentration is described in U.S. Pat. No. 7,459,594. It is a catalyst with partial oxidation, where the product gas and the oxidant are mixed just above the catalyst layer, where the oxidant is fed through a layer of cold plasma, which also ignites the mixture immediately. The system works well at lower flows where sufficient homogenization of the mixture can be ensured. At higher flows, however, anomalies occur, which means that some parts of the catalyst undergo intense oxidation and some do not. This is mainly due to the action of plasma and point supply of oxidant, which are limited to an ever narrower band or cross-section of the increase in flow, so that the oxidant and product gas before entering the catalyst do not provide a sufficiently homogeneous mixture. As a result, high temperatures occur in certain parts of the catalyst, where large amounts of fixed carbon begin to be emitted in the form of soot or carbon dust, and part of the product gas and / or air passes through the catalyst in unreacted form, ie with tar present.

Homogenization of a mixture for partial oxidation

In the catalytic conversion of tars by a partial oxidation process, an appropriate amount of oxidant (oxygen or air) is added to the product gas before entering the catalyst. There is usually extremely little oxygen in this mixture, 1 to 3 percent. It is extremely important that the mixture is as homogeneous as possible before the partial oxidation reactions in the catalyst are triggered. The homogeneity of the mixture prevents the occurrence of the hot spots described above so that the problems described above do not occur. The solution is to separate the mixing part from the reaction zone with a suitable flame arrestor as described in US Pat. No. 2007/0212276, where the catalyst consists of a chamber to which the product gas and oxidant are supplied with an integrated flame arrestor in the form of a metal foam sponge and stationary stirrers. , and catalyst vessels. The described solution is used for the conversion of pure long hydrocarbons into shorter products, as well as for the production of H2 and CO (synthetic gas), for example from methane, but is not suitable for processing product gas from a gasification plant containing higher or lower tar concentration. loaded with dust, as the flame barrier or stirrer described in this patent would be quickly blocked by the application of tar and dust, and at the same time such a device also represents a large pressure barrier and a place with intense heat dissipation, which is undesirable.

Device component integration

Typically, clean synthesis gas production systems are positioned as a set of stand-alone devices that follow the flow of the process. The integration of the components into the whole is presented, for example, in U.S. Pat. No. 8,936,886, which describes a system for producing pure synthesis gas using a countercurrent gasifier, immediately followed by a device for thermally converting tars to product gas and thus producing pure synthesis gas. gas. The operating temperature in the second reactor is achieved by recuperation, and in particular by the addition of an oxidant to the (crude) product gas, which triggers the complete oxidation of part of the product gas in the gas stream itself. Due to the required long retention times, a relatively large amount of oxidant is required for the process of thermal conversion of tars, which significantly reduces the calorific value of the purified synthesis gas, so this system is more useful for heat production.

An example of the integration of a carburetor and a catalyst is also the patent CN 2008 / 10.021.485, where the catalyst part is located directly above the carburetor and is separated only by a funnel-shaped narrowing of the vessel. An S-resistant catalyst (dolomite added CaO) was used. Immediately after the gasification phase is the catalytic conversion phase followed by gas purification. The described system produces a product gas with the lowest possible tar content, which limits the range of gasification material used. Also, the catalyst cannot operate with a partial oxidation process, as the optimal supply of oxidant and preparation of a homogeneous mixture is practically impossible.

Explanation of terms used

In the following description of the invention, the terms "product gas" and "synthesis gas" are used. For the purpose of describing the present invention, a "product gas" is a gas coming from a gasifier to a catalytic reactor, where it is processed into a "synthesis gas".

The essential difference between a product gas and a synthesis gas is that the product gas contains tars and dust particles, while the synthesis gas consists essentially of CO and H2, without tar and dust particles it does not need to be further cleaned.

Furthermore, the term "pure synthetic gas without water or moisture" means a tar-free gas mixture consisting of CO, H2, and additionally CO2, CH4 and a minimum moisture content.

Short description of the pictures

The present invention is further described by means of the accompanying drawings, which show:

Figure 1: Schematic representation of a gasification line according to the present invention;

Figure 2: first part of a line according to the present invention (dosing of gasification material and countercurrent gasifier);

Figure 3: second part of the line according to the present invention (catalytic reactor and technological preparation of synthetic gas);

Figure 4: Schematic representation of the integration of a catalytic reactor and a flow carburetor;

Figure 5: Schematic representation of the integration of a catalytic reactor with a single catalyst outside the countercurrent gasifier according to the present invention;

Figure 6: Schematic representation of the integration of a catalytic reactor with several catalysts outside the countercurrent gasifier according to the present invention;

Figure 7: Schematic representation of the integration of a multi-catalyst catalytic reactor in a countercurrent carburetor cover according to the present invention;

Brief description of the invention

The present invention solves the technical problem by introducing a device that enables gasification of solid materials with carbon content and conversion of tars into CO and H2 or synthetic gas.

The device for gasification of solid materials with carbon content according to the present invention combines two types of reactors that can be built and increased in any size, namely:

carburetor of carbon-containing materials such as coal, wood and biological biomass, municipal and special waste, sewage sludge or biogas, materials with S and / or Cl content, such as brown coal or rubber producing high gas product gas concentration of tars or hydrocarbons.

a catalytic reactor that converts the resulting tars / hydrocarbons in the product gas to CO and H2 and provides a synthesis gas with a significantly higher hydrogen content and no tar at the outlet, so that the synthesis gas meets the quality standards for further use, for example in internal combustion engines. combustion or as a feedstock for the synthesis of hydrocarbons.

The device according to the present invention is schematically shown in Figure 1 and in detail in Figure 2 and Figure 3 and consists of the following essential parts:

mixer,

- first transport system, second transport system,

- gasification reactor, catalytic reactor, and synthetic gas treatment system.

The device according to the present invention consists of:

- a mixer 1 of gasification material, comprising dosing systems 2, 3, 4, 5, a device for detecting the presence of compounds S and Cl in the gasification material, a weighing device and a grinding device;

first transport system 6,

- a second conveyor system 50, a carburetor 8 surrounded by a first heat exchanger 28 and comprising an upper part 14, a discharge pipe 15, a grate 9, a rotating shovel 52, a third conveyor system 53, a cell barrier 11, an ignition system 56, a supply system 12 , 13, temperature meter 57 and raw material level meter 58,

- a catalytic reactor consisting of a mixing part 16, with inlets 17, 18, 19, a distributor 20, a catalyst 21, a flame arrestor 22, an ignition chamber 23, ignition elements 24 and a catalyst core 25 surrounded by heaters 26, a second heat exchanger 30, the third heat exchanger 33, and

- a dehumidifier 36, wherein the second heat exchanger 30, the third heat exchanger 33 and the dehumidifier 36 form a synthesis gas treatment system.

These elements of the device are interconnected in such a way that the device allows the process for gasification of solid materials with carbon content.

The gasification material mixer 1 contains dosing systems, namely a gasification material dosing system 2, a dosing system 3 for dosing optional additives to the gasification material (such as wood sawdust, sewage sludge or heavy municipal waste fraction), a dosing system an adsorbent dosing system 4 for binding S and C1 and a water dosing system 5 consisting of a dosing valve with a nozzle. Each dosing system 4, 5 has its own hopper 40 with a dosing valve 41.

Furthermore, the gasifier material mixer 1 comprises a device for detecting the presence of compounds S and C1 in the gasification material, a device for weighing the dosage materials and a device for optionally grinding the gasification material (not shown).

Said gasifier mixer 1 has an outlet opening in the lower part, which is closed by a flap 43, through which the prepared gasification raw material is fed to the inlet part 44 of the first transport system 6, which in the described embodiment is a lifting auger that lifts the raw material above the cell. barrier 7. The cell barrier 7 consists of an upper valve 45 and a lower valve 46, one of which is always closed when the gasification feedstock passes through the cell barrier. The operation of valves 45, 46 is regulated by an upper 47 and a lower 48 level switch. The cell barrier 7 prevents the spread of return fire to the supply of gasification raw material or prevents the leakage of product gas from the device.

The raw material for gasification through said cell barrier and through the space 49 below the cell barrier falls on a second transport system 50, which is in a preferred embodiment a dosing auger. Said space 49 below the cell barrier is conical in such a way that it expands downwards and therefore no gasification of the raw material for gasification can occur.

Said dosing screw 50 dispenses the raw material for gasification into the carburetor 8 and is inclined so that its highest point is in the carburetor 8, thus preventing the occurrence of return fire from the carburetor 8.

The dosing auger 50 dispenses the gasification feedstock onto the grate 9 of the carburetor 8, through the center of the grate 9 so that the material in the middle of the carburetor 8 moves upwards and along the walls of the carburetor 8 backwards downwards towards the grate 9.

Said carburetor 8 has a rotating shovel 52 in the space 10 under the grate 9, which pushes the ash generated during gasification, which falls through the grate 9, to a third conveying system 53, which is preferably an auger which removes the ash from the appropriate cell barrier 11. devices to the appropriate collector 54.

Said carburetor 8 further comprises an ignition system 56, such as a hot air blower system mounted above the grille 9.

The carburetor 8 further comprises a system 12 for supplying the first oxidant located below the grate and equipped with a dosing nozzle 55 and a water or steam supply system 13 located below the grate and equipped with a dosing nozzle 55.

The carburetor 8 further comprises a temperature meter 57 located below the grate to regulate the amount of water or water vapor supplied to the carburetor 8 and a feedstock level meter 58 in the carburetor 8 to control the amount of gasification feedstock on the carburettor grate 8.

The carburetor 8 is designed as a pressure vessel so that the gasification process takes place in the overpressure mode. This provides better opportunities for managing process conditions. The passages of the gasification feedstock to and from the carburetor 8 are equipped with cell barriers 7 and 11, which allow the passage of said feedstock under the pressure regime.

The carburetor jacket 8 is hollow and serves as the first heat exchanger 28, as will be described below.

The described embodiment of the carburetor 8 allows the use of a wide range of carbon-containing material for gasification, such as coal of all kinds, wood biomass or biomass of plant origin, municipal or industrial waste, sewage sludge or biogas plants or any other combustible materials. Gasification materials must have an appropriate particle size, so they are usually in the form of sawdust, pellets or chips, with heterogeneity of material composition being desirable. We cannot gasify the powder itself, but we can add a certain proportion of it to the gasification material. There is also a limitation on liquid or highly flammable substances that need to be properly mixed with a dry carrier, such as wood sawdust or other suitable absorbent substance. Gasification materials do not need to be dried separately, and water is added if necessary.

In the gasification process that takes place in the carburetor, a product gas is formed, which collects in the upper part 14 of the carburetor 8 and is discharged through the outlet pipe 15 on the carburetor cover 8 into the mixing part of the catalyst 16.

Said mixing 16 part of the catalytic reactor is equipped with a system 17 for the supply of the second oxidant, a system 18 for the supply of water or water vapor and a system 19 for the supply of ignition gas. The entire mixing part of the catalytic reactor 16 is designed to provide a homogeneous substoichiometric mixture of product gas and oxidant. A homogeneous posteichiometric mixture of product gas and oxidant provides a stoichiometric ratio of 0.3-0.5 (preferably 0.4) based on the proportion of tars, expressed as CioHg, consumed during partial oxidation to achieve a homogeneous temperature field in the space in front of the catalyst core 25.

The mixture of product gas and oxidant through the manifold 20, through the flame barrier 22 and through the ignition chamber 23 is led to the catalyst core 25, catalyst 21, where a homogeneous partial oxidation of tars in the product gas is established, tars are converted into CO and H2 or pure synthesis gas , which ensures a sufficient rise in the temperature of the product gas, which can then support the endothermic process of catalytic steam reforming of the remaining tars.

The catalyst core 25 is made of a linear ceramic support that is resistant to temperature shocks and is sufficiently porous to be subjected to a catalytic layer, such as a layer of a suitable metal. The catalyst core 25 comprises a plurality of parallel honeycomb channels running in the direction of the product gas flow, where the cross section of said channels is large enough to allow the passage of solid inorganic particles or ash that the product gas may contain.

The catalyst core 25 can also be made in the form of granules, which is not the case for gases containing solid inorganic particles.

The catalyst core 25 of the device according to the present invention has a uniform temperature in all parts, which is achieved by a homogeneous mixture of oxygen, product gas and water vapor in the mixing part 16 of the catalytic reactor, separated from the catalyst core 25 by a flame barrier 22. in the form of a honeycomb as described above for the catalyst core 25.

Flame retention in the flame arrestor 22 is achieved exclusively by increasing the velocity of the product gas-oxidant mixture, for which the proper homogeneity of said mixture is very important, thereby fully maintaining the temperature of the product gas.

The mixing part of the catalytic reactor 16 is also adapted to the high concentration of tars and / or dust in the product gas, which is carried out without passive stirrers only by appropriate design of the mixture (distributor 20) in the catalyst 21 and ensures adequate homogeneity of the mixture.

The length of the mixing part of the catalytic reactor 16 without passive mixers is significantly shortened by dividing the catalyst 21 into several smaller units, and the distributor 20 already provides a homogeneous mixture with its shape, which is also reflected in lower heat losses.

Said outlet pipe 15 is surrounded by heaters 59 which are equipped with temperature sensors. Before starting the process with said heaters 59, the outlet pipe 15, the mixing part of the catalyst 16 and the distributor 20 are heated to an operating temperature of between 300 ° C and 400 ° C.

Said catalyst core 25 of the catalyst 21 is surrounded by heaters 26, with which, before the start of the process, the catalyst core 25 is heated to an operating temperature of the catalytic reaction of about 700 ° C.

Said catalyst core 25 has a temperature meter 60 in the middle, with which the temperature of the catalyst core 25 is monitored.

To heat the catalyst core 25, a mixture of ignition gas and another oxidant can be used instead of heaters 60, which are fed through said supply systems 17, 19 to the outlet pipe 15. Said mixture ignites after passing through the flame barrier 22 on the ignition elements 24 and just above the catalyst. core 25.

Said ignition gas is also used to clean any soot from the catalyst core 25.

When the catalyst core 25 is heated to the initial operating temperature, a mixture of product gas and oxidant is introduced into the catalyst 21, which is ignited by the ignition elements 24 in the ignition chamber 23 just above the catalyst core 25, where the catalytic conversion process takes place. In an atmosphere with a low oxygen content, which depends on the concentration of tars in the product gas and usually amounts to 1 to 2 percent by volume (or more or less), two reactions take place that are important for the process itself:

1. partial oxidation (exothermic process),

2. steam reforming (endothermic process),

The first reaction ensures a sufficiently high operating temperature and is the leading reaction, while the second reaction provides the conditions for the formation of a higher quality synthesis gas with a higher concentration of CO and H ₂ and a higher H ₂ / CO ratio. The tar content in the product gas must be at least sufficient to cover the energy needs of the catalyst operating temperature maintenance system.

The higher concentration of tars also eliminates the significant disadvantage of using low-tar product gases, where oxygen in the absence of tars during the heat supply phase for the catalytic vapor reforming process begins to bind to already formed H2 and CO in the full oxidation reaction to CO2 and H2O. deterioration of the calorific value of the gas, higher temperatures develop, which may also be unevenly distributed, and unbound carbon in the form of soot is formed, which blocks the action of the catalyst (clogs the catalyst). The process is therefore controlled at an appropriate concentration of tars so that it is autothermic. Catalyst 21 is adequately insulated 61 to reduce heat loss.

The synthesis gas from the catalyst 21 is passed through a connecting pipe 62 to the collector 27 and on to the first heat exchanger 28 surrounding the carburetor 8, where said synthesis gas transfers part of the heat to the fuel column 51 in the carburetor 8.

The device according to the present invention further comprises a second heat exchanger 30, to which synthesis gas is fed from the first heat exchanger 28.

Said second heat exchanger 30 is connected to the first heat exchanger 28, to the third heat exchanger and has an opening 63 for the entry of fresh oxidant 31 and an opening and 64 for the discharge of heated oxidant connected to the supply 17 of the second oxidant at the mixing part 16 of the catalytic reactor.

In the second heat exchanger 30, the synthesis gas transfers part of the heat to an oxidant 31, such as air, which is used in the process as a second oxidant 17 for the catalytic reaction. The oxidant 31 enters the second heat exchanger 30 in the opposite direction from the synthesis gas flow, in the case described above, through the inlet 63 and leaves it below, through the outlet 64, after which it is metered into the mixing part of the catalyst 16 through the supply of the second oxidant 17.

The synthesis gas cooled to the water condensation limit is led from the second heat exchanger 30 through the pipe 32 to the third heat exchanger 33, where it is cooled below the water condensation limit.

Said third heat exchanger 33 is connected to a second heat exchanger 30, to a steam cooler 36, and has an opening 64 for the inlet of the heat dissipation medium 34 and an opening and 66 for the outlet of the heat dissipation medium.

Said heat dissipation medium 34 in the third heat exchanger 33 is a liquid, such as water, which in the described case enters the third heat exchanger 33 below through the inlet 65 and exits above through the outlet 66 while the synthesis gas travels to the opposite directions.

The synthesis gas cooled below the water condensation limit is then fed through a pipe 35 to a dehumidifier 36. The upper part of the carburetor, the product gas outlet pipe, the catalyst mixing part, the catalyst, the catalyst outlet pipe and the second and third heat exchangers are thermally insulated.

Said dehumidifier 36 is connected to a third heat exchanger 33, comprises a condensation barrier 37 for removing moisture from the synthesis gas, and has a condensed water collection tank 67 at the bottom, equipped with a condensed water drain valve 68 and a water level meter 69. in the condensed water tank 67 which controls said valve 68.

Furthermore, said dehumidifier 36 has an opening 39 for the synthesis gas outlet at the top. The collected condensed water is filtered and used in the process which takes place in the described device for adding water to the mixer 1, to the carburetor 13, to the mixing part of the catalyst 18 and for cooling 34.

Synthetic gas, tar-free and low-moisture, exits the device through an opening at the top of the dehumidifier 39. The resulting synthesis gas is then used as a feedstock, in chemical synthesis processes (eg Fischer-Tropsch reactors, methanation or methanol synthesis), as technical gases or as an energy source for energy production.

The entire construction of the device according to the present invention is carried out in the overpressure mode, and it is also possible to carry out the described device in the underpressure mode. All components of the device are equipped with safety outlets.

Figures 4 to 7 schematically show embodiments of the device according to the present invention with respect to different types or sizes of carburetors 8 and catalysts 21.

Figure 4 shows the installation of the catalyst 21 in configuration B, with several catalyst units connected in parallel on a flow biogasm gasifier 70. The gasification material enters through the upper part of the carburetor 70. The first oxidant is blown through the inlet 12 into the lower part of the carburetor 70 from which part of the ash and product gas exits at the lower part 71 and is discharged through the outlet 15 into the cyclone 72 added to the system. because the product gas is loaded with dust or unreacted carbon in the form of soot. From said cyclone 72, at the bottom 73, the remaining part of the ash protrudes. The product gas is introduced into the mixing part 16 of the catalytic reactor, into which the second oxidant is fed through the inlet 17. In the manifold 20, the mixture is separated into individual catalysts 21, where the tars are converted to CO and 1¾. The synthesis gas is collected in the collector 27 and cooled in the heat exchanger 33, and exits through the outlet 39.

Figures 5 and 6 show the integration of the countercurrent carburetor 8 according to the present invention and the catalyst 21 in the configuration A (Figure 5) and in the configuration B (Figure 6). In both cases, the gasification material 2 enters the carburetor 8 through the cell barrier 7. The first oxidant is dosed into the lower part of the carburetor 8, through the inlet 12 and water or water vapor through the inlet 13, and the ash is removed through the discharge opening 71. The tar-rich product gas is mixed with another oxidant in the mixing part of the catalytic reactor 16. Figure 5 shows the installation of the catalyst 21 in an embodiment with one catalyst unit, and Figure 6 with several parallel catalyst units, where the gas-oxidant mixture is divided into several units in the manifold 20 and after conversion in individual units, when the synthesis gas is formed, combined into collector 27. The hot synthesis gas is led to the first heat exchanger 28, which surrounds the carburetor 8, where it emits part of the heat. From the first heat exchanger 28, the synthesis gas is then led 29 to a synthesis gas cooling device.

Figure 7 shows the full integration of the countercurrent carburetor 8 according to the present invention and the catalyst 21 in the configuration B, ie with several parallel catalyst units, where the catalyst is located just above the carburetor 8. Here again, the gasification material 2 enters the carburetor through the cell barrier 7. 8. Dosing the first oxidant into the lower part of the carburetor through the inlet 12 and water or water vapor through the inlet 13, and removing the ash through the outlet opening 71. The product gas in the middle of the carburetor enters directly into the mixing part of the catalyst 16, where another oxidant is fed through the inlet 17. The mixture is then divided into individual catalyst units 21 at the manifold 20, which is completely at the top of the device. The resulting synthesis gas is fed to the first heat exchanger 28, which surrounds the carburetor 8, where it emits part of the heat and is forwarded 29 to the gas cooling device. .

The advantages of the device according to the present invention are the following:

due to the higher permissible concentration of tars in the product gas, the device enables gasification of low-quality or more complex materials with a high content of moisture and / or dust, which significantly expands the applicability of said device;

the device enables slow gasification of materials at lower temperatures in the presence of moisture and adequate backfilling of the material, which creates a filter (adsorption) zone and enables chemical reaction of the adsorbent with S and / or Cl compounds and thus removal of S and / or Cl compounds during gasification of materials. contain these two elements; due to the catalytic conversion of the product gas with a higher tar content, the device allows the use of a countercurrent carburetor, which is the simplest type of carburetor;

the device enables the process of partial oxidation of tars for internal heating of a catalytic reactor without increasing the content of inert components in the gas (eg CO2), followed by a catalytic process of steam reforming, which linearly increases the H2 / CO ratio in the synthesis gas. Thus, the tar conversion process is autothermic;

the device enables catalytic conversion in a catalyst with wide channels, so it is also possible to process dust-laden gas from a countercurrent carburetor;

the device does not cause the formation of carbon or soot, which would be excreted in the ash or in the product / synthesis gas, because the carbon, by the process of partial oxidation before catalytic conversion, is converted into a gaseous state;

the device allows a process to be carried out that causes lower emissions compared to incineration, and the residues after gasification are inorganic ash and condensate water, which is used as process water in the process itself;

- the device allows a process whose product is pure synthesis gas, free of tars, compounds S and Cl and dust particles and with low concentrations of moisture, CH4 and CO2, in the case when air is used as the first oxidant, as well as N2, where said synthetic gas ready for further use.

The device according to the present invention is described and shown in the accompanying figures by means of concrete embodiments, which in no way limit the invention itself. Various versions of the described device are also possible, but they will be immediately clear to those skilled in the art.

Claims (7)

Patent claims 1. A device for gasifying solid materials with a carbon content with a pronounced concentration of tars and their catalytic conversion into carbon monoxide and hydrogen, characterized in that they consist of: gasifier material mixer (1) comprising a gasification material dosing system (2), a gasification material dosing system (3) for dosing optional gasification material additives, an adsorbent dosing system (4) and a dosing system (5) water, a device for detecting the presence of compounds S and C1 in the gasification material, a weighing device and a grinding device; - the first transport system (6); other transport system (50); - a carburetor (8) surrounded by a first heat exchanger (28) and comprising an upper part (14), a discharge pipe (15), a grate (9), a rotating shovel (52), a third conveyor system (53), a cell barrier (11), an ignition system (56), a first oxidant supply system (12), a water or steam supply system (13), a temperature meter (57) and a raw material level meter (58); - catalytic reactor, which contains a mixing part (16) which is configured so as to provide a homogeneous podstehiometrijsko mixture of product gas and an oxidant with a stoichiometric ratio of from 0.3 to 0.5, preferably 0.4, with respect to the proportion of tars, expressed as C ₀ H _8, which partial oxidation, based mainly on the partial oxidation of tars, takes place behind the flame barrier (22), which allows to achieve a homogeneous temperature field in the room in front of the catalyst core (25) and thus prevents the formation of unbound carbon, the supply system (17) , supply system (18) for water or steam supply, supply system (19) for ignition gas supply, distributor (20), catalyst (21), flame arrestor (22), ignition chamber (23), ignition elements (24) and a catalyst core (25) surrounded by heaters (26) and having a temperature meter (60) in the middle to control the temperature of the catalyst core (25), a second heat exchanger (30), a third heat exchanger (33), and - a dehumidifier (36) comprising a condensation barrier (37) for removing moisture from the synthesis gas and having a condensed water collection tank (67) in the lower part equipped with a condensed water drain valve (68) and a meter (69 ) of the water level in the tank (67) which controls said valve (68). Device according to claim 1, characterized in that: said first conveyor system (6) and said second conveyor system (50) are located between said mixer (1) and said carburetor (8), there is a cell barrier between said first conveyor system (6) and said second conveyor system (50) (7), through which the material from the first conveyor system (6), through the space (49), falls on said second conveyor system (50), said first conveyor system (6) and said second conveyor system in a preferred embodiment are made in the form lifting auger. Device according to Claim 1 or 2, characterized in that: - the carburetor (8) is surrounded by a hollow jacket, which represents the first heat exchanger (28), which is connected to the outlet part of the catalyst (21) via a collector (27) and a connecting pipe (62), from where the synthetic gas enters said first exchanger. heat (28) and transfers part of the heat to the fuel column (51) in said carburetor (8) - the carburetor (8) is connected to a second heat exchanger (30), where synthetic gas enters from the first heat exchanger (28), where in said second heat exchanger (30) said synthetic gas part of the heat is transferred to the second oxidant (31). this cools to the limit of water condensation and the heated second oxidant is led to the stirring part (16) of the catalytic reactor; - said second heat exchanger (30) is connected to a third heat exchanger (33), where synthetic gas cooled to the water condensation limit enters from the second heat exchanger (30), where said synthetic gas transfers part of the heat to the heat transfer medium (34), and it cools below the water condensation limit; - said third heat exchanger (33) is connected to a dehumidifier (36), where synthetic gas cooled below the water condensation limit enters from the third heat exchanger (33), where said condensation barrier (37) removes condensed water cooled from the synthetic gas. gas, free of tars and dust particles, compounds S and C1 and with low concentrations of moisture, CH4 and CO2, in the case when air is used as the first oxidant, as well as N2, exits the said dehumidifier (36) through the outlet opening (39) . Device according to claim 1, 2 or 3, characterized in that said catalyst core (25) is made of a linear ceramic support which is resistant to temperature shocks and is sufficiently porous to be subjected to a catalytic layer, such as, for example, layer of the corresponding metal and that the catalyst core (25) contains a plurality of parallel honeycomb channels running in the direction of the product gas flow, where the cross section of said channels is large enough to allow the passage of solid inorganic particles or ash by the product gas. may contain. Catalytic reactor, characterized in that it comprises a mixing part (16), a supply system (17) for the supply of a second oxidant, a supply system (18) for the supply of water or water vapor, a supply system (19) for the supply of ignition gas, a distributor (20), further characterized in that it comprises two or more catalyst units (21) connected in parallel, wherein each catalyst unit comprises a flame arrestor (22), an ignition chamber (23), ignition elements (24), a catalyst core (25). according to claim 4, surrounded by heaters (26) and having a temperature meter (60) in the middle to control the temperature of the catalyst core (25), wherein the mixing part of the catalytic reactor (16) is configured to provide a homogeneous substoichiometric mixture of product gas and oxidant, with a stoichiometric ratio of 0.3 to 0.5, preferably 0.4, based on the proportion of tars, expressed as CioHg, whose partial oxidation, based mainly on the partial oxidation of tars, takes place behind the flame arrestor (22), allowing up to reaching a homogeneous temperature field in the space in front of the catalyst core (25) and thus preventing the formation of unbound carbon. Device according to any one of claims 1 to 4, characterized in that it comprises a catalytic reactor according to claim 5. Device according to any one of claims 1 to 5, characterized in that it is configured to carry out a process for gasifying solid materials with a carbon content by converting tars into carbon monoxide and hydrogen, wherein the device: due to the higher permissible concentration of tars in the product gas, it enables the gasification of low-quality or more complex materials with a high moisture and / or dust content, which significantly expands the applicability of said device; - enables slow gasification of materials at lower temperatures in the presence of moisture and adequate backfilling of material, which creates a filter or adsorption zone and enables chemical reaction of the adsorbent with compounds S and / or Cl and thus removal of compounds S and / or Cl during gasification of materials. contain these two elements; due to the catalytic conversion of the product gas with a higher tar content, allows the use of a countercurrent carburetor, which is the simplest type of carburetor; enables the process of partial oxidation of tars as the main source for internal heating of the catalytic reactor, followed by the catalytic process of steam reforming, which linearly increases the H ₂ / CO ratio in the synthesis gas with higher tar content and thus favors higher tar content at the carburetor outlet. ; allows catalytic conversion in a wide-channel catalyst, which also allows the treatment of dust-laden gas from a countercurrent carburetor; does not cause the formation of carbon or soot, which would be excreted in the ash or in the product / synthesis gas, because the carbon, by the process of partial oxidation before catalytic conversion, is converted into a gaseous state; allows the process to be carried out, which causes lower emissions into the environment compared to incineration, and the residues after gasification are inorganic ash and condensate water, which is used as process water in the process itself.