SI25770A - Process of gasification of solid materials that contain carbon, with an emphasized tar concentration and their catalytic conversion into carbon monoxide and hydrogen - Google Patents

Abstract

The present invention discloses a process for gasifying solid carbon-containing materials with a high concentration of tars and their catalytic conversion to carbon monoxide and hydrogen, comprising preparing a gasification feedstock comprising dosing a gasification material, optional additives, adsorbent and water, gasifying said feedstock, single or multi-phase purification of the product gas, conversion of tars into synthesis gas and conduction of the synthesis gas through a series of heat exchangers and a dehumidifier. The process enables a higher permissible concentration of tars in the product gas, which enables autothermal catalytic conversion and at the same time gasification of low-quality or more complex materials with high moisture and / or dust contents, thus significantly expanding the applicability of the gasification process. The result of the process is a synthesis gas, free of tars, compounds S and Cl and dust particles and with low concentrations of moisture, CH4 and CO2, when air is used as the first oxidant, as well as N2. Said synthetic gas is suitable for use as raw material but energy. Residues after gasification are inorganic ash and condensate water, which is used as process water in the process itself.

Description

Process for gasification of solid materials with carbon content _f with pronounced concentration of tars and their catalytic conversion into carbon monoxide and hydrogen

Field of the invention:

The subject of the invention is a process for gasification of carbon-containing materials for the production of tar-free synthesis gas.

Description of the technical problem:

The tar content in the produced gas is still today the main problem of all gasification systems intended for the production of combustible synthesis gas. We know some measures to reduce tar, which can be divided into:

- primary measures (measures inside the carburetor), which rely on appropriate control strategies or maintenance of the conditions of the gasification process and current dynamics in the carburetor, so that the formation of tars is minimal. As a result, technological solutions limit operation in terms of system flexibility, the possibility of different dimensions of the device, in addition, the devices are extremely limited in the selection and preparation of materials for gasification, and as a by-product can produce large amounts of coal and operate in very limited operating conditions. Although primary measures can significantly reduce the tar content, it is considered impossible to completely remove them without the use of secondary measures.

- secondary measures (measures after the carburetor), which rely on the post-treatment of the product gas by different methods (heat treatment, catalytic treatment, washing). Such measures also have certain shortcomings: they are not efficient enough, they are too expensive, they negatively affect the calorific value of the gas, or they transfer the problem of tars to wastewater treatment. In the case of catalytic secondary measures, energy for endothermic processes is in most cases obtained from an external heat source (hot gas supply or electric heaters).

All existing gasification processes are currently adapted and optimized within the thermodynamic capabilities for the production of product gas with the lowest possible tar content, as these cause technical problems in gasification systems and further applications. The tar content in the product (synthesis) gas ranges from 0.1% (flow gasifiers) to 20% (counterflow gasifiers) or more (in pure pyrolysis processes). The energy value of the product (synthesis) gas ranges from 5 MJ / Nm to 15 MJ / Nm ³ and is considered a low or medium calorific gas compared to natural gas (35 MJ / Nm ³ ). If air is used as the oxidant, the product (synthesis) gas contains about half of N2. The relative amount of CO, CO2, H2O, H2 and hydrocarbons depends on the stoichiometry of the gasification process. The air / material ratio for gasification in the gasification process is generally in the range of 0.2 - 0.35, but if steam is used as the oxidant, the steam / material ratio is about 1. Actual amount of CO, CO2, H2O, H2, tar or hydrocarbons depends on the partial oxidation of volatile hydrocarbons shown by the following equation:

C _n H _m + (n / 2 + m / 4) O _{2 n} CO + (m / 2) H ₂ O.

Normally, in gasification processes, in order to minimize the tar content in the product (synthesis) gas, the most homogeneous and dry materials are used, which are properly treated and purified, and in particular the use of materials containing substances with elements S and Cl is avoided. The problem of the presence of S as well as C1 in the fuel is well known, as both cause corrosion on the equipment and dangerously pollute the environment. The presence of S and Cl in fuels is usually solved outside the thermal conversion process, followed by washing of the product or flue gas (together with other secondary tar removal measures) or before it by removing substances with S and Cl content from the input materials for thermal conversion . Methods of removing S and Cl during the thermal combustion process itself are also known, especially in the energy use of fuels or in the production of cement. In these cases, the method of adding various additives and adsorption substances containing Ca for a long time has been used in order to improve the fuel or the best possible excretion of S and Cl into the ash already in the combustion process.

State of the art

The process of gasification and conversion of tars is described in US Pat. No. 8,936,886 B2, according to which the fuel is dosed into a countercurrent gasifier in which the process conditions are optimized for the production of product gas with the lowest possible concentration of tars. The tars that are nevertheless formed are then converted in the next phase by a thermal conversion process. Optimizing the production of product (synthesis) gas with as little tar as possible limits the possibility of using heterogeneous and moist raw materials, and the use of thermal conversion significantly reduces the energy value of synthetic gas.

Methods for removing elements S and C1 by adding an absorbent to a fuel are already described in U.S. Pat. Nos. 174,348, EP 1765962, U.S. Pat. No. 6,599,123 and U.S. Pat. All the above examples speak of the use of additives in the combustion process, which is a rapid chemical reaction, with large temperature gradients, when the fuel dries, gasifies and oxidizes very quickly. In the described conditions of rapid reactions or very high temperatures, other chemical reactions do not have enough time to proceed optimally, as retention times are extremely short, especially compared to gasification, where drying and gasification reactions take place over a few seconds. As a result, the gasification effects of binding S and C1 with, for example, Ca or Mg, to solid compounds are significantly more effective, so that practically all of S and C1 can be removed already in the gasification phase, with ash.

A possible integrated solution of the gasification process, where a catalyst is used to convert the tar and at the same time remove the S and C1 elements by adding an adsorbent, is presented in patent EP 0512305, which discusses the use of RDF raw material (processed municipal waste) for gasification. A floating carburetor is used. The catalytic conversion and removal processes S and C1 also take place in a floating layer, where a powder of a mixture of limestone, dolomite and alkaline adsorbent is added to the gas stream, circulating through the system at all times. However, the product gas is loaded with ash and after catalytic reactions it must be cleaned with particle separators, water showers and filters. The fuel must be properly prepared or crushed into small particles, and the process conditions are demanding.

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 product gas and synthesis gas is that product gas contains tars and dust particles, while synthesis gas consists mainly of partial oxidation products (CO and H2) and inert components that depend on the oxidant used, and above all it is free of tars and dust particles and does not need to be further cleaned before further use for the synthesis of raw materials or as a fuel.

Hereinafter, the term "pure synthetic gas without water or moisture" means a gas mixture which is free of moisture and consists of CO, H2, and additionally CO2, CH4 and a minimum moisture content.

Short description of the attached pictures:

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

Figure 1: schematic representation of the gasification process according to the present invention;

Figure 2: schematic representation of the elimination process of components S and Cl;

Figure 3: Schematic representation of the integration of the gasification process, catalytic conversion and precipitation of the S and Cl components.

Description of the invention

The present invention solves the problem of the presence of tar formed during the gasification of carbon-containing materials by adapting the gasification conditions to emphasize the formation of tars or hydrocarbons in the product gas, where these increased concentrations of tars (or hydrocarbons) represent the optimal input reactant for catalytic conversion. into the synthesis gas taking place in the catalytic reactor. The process described can be carried out with any type of gasifier, provided that the formation of a minimum concentration of tars in the product gas of at least 4 g / Nm ³ to 6 g / Nm ³ , preferably at least 5 g / Nm ³ , as well as a suitable the product gas outlet temperature achieved by the process conditions themselves or by energy supplied from the outside, which ensures that the hydrocarbons do not condense before entering the catalytic reactor. In particular, countercurrent carburetors of all kinds are suitable for gasification in the manner described. For the conversion of tars or hydrocarbons in a catalytic reactor, any catalyst intended for the conversion of hydrocarbons into hydrogen and carbon monoxide can be used. This simplifies the gasification process conditions, which are much easier to manage, and extends the range of gasification feedstocks used to feedstocks where heterogeneity of composition and moisture are desirable. For the operation of a catalytic reactor, the presence of higher concentrations of hydrocarbons means more optimal process conditions, which ensures a significant improvement in the conditions for the conversion of all hydrocarbons into hydrogen and carbon monoxide and thus pure synthesis gas.

The essential feature of the process according to the present invention and thus also the essential difference from all such processes according to the state of the art is that it is desirable in the heterogeneity of the gasification material, as well as the presence of moisture in the gasification material. we produce higher concentrations of tars, which are crucial for the autothermic course of catalytic conversion of tars without increasing the inert components in the resulting gas (eg N2 and CO2). This is achieved by dosing or the presence of water or water vapor, which plays a key role in the process:

water, which is present in the gasification material by evaporation, lowers the gasification temperature in the carburetor in the upper layers, or enables processes in which more tars are formed, and at the same time supports the process of binding S and / or C1 with the adsorbent;

water or water vapor dosed under the carburettor grate lowers the temperature in the lower layers and supplies additional oxygen and hydrogen to the process;

water vapor, which evaporates in the process of drying and pyrolysis and is an integral part of the product gas, in the catalytic conversion with steam reformer enriches the synthesis gas with additional hydrogen.

In order to generate thermal energy in the gasification process, partial oxidation of materials with a carbon content in CO and, to a minimum, oxidation of materials to carbon dioxide, CO2, take place. Under the oxidation zone, in addition to the oxidant, we also supply water or water vapor, which regulates the gasification temperature, and especially water vapor is an additional source of hydrogen in cases of gasification of carbon-containing materials from less volatile compounds, such as coal. sufficiently high concentrations of hydrocarbons in the product gas can be formed. A small amount of oxidant is then added to the product gas and taken to a catalytic reactor, where a catalytic reaction of partial oxidation and also steam reforming takes place with the help of a catalyst, with which the tars are decomposed into CO and H ₂ . The process in the carburetor and in the catalytic reactor is conducted in such a way that it is autotherm.

The present invention also solves the elimination of components S and C1 already within the gasification process. The raw material with the appropriate moisture content must be used, and the process must be managed in such a way that it takes place at lower temperatures and with longer retention times in the drying and pyrolysis phases, which allows extremely efficient binding of elements S and C1 with adsorption material (containing for example Ca or Mg), and their excretion into the ash. With this, the range of materials suitable for gasification was extended to the field of municipal and other waste or materials that are suitable for gasification and may contain substances with S and Cl content.

Expansion of the range of useful materials for gasification is achieved by adding adsorption material, which in the conditions of gasification of wet material, sulfur and chlorine already binds in the carburetor, namely in such compounds, which are already separated in the carburetor in solid form into ash. gaseous compounds with elements S and C1 and their transition to the catalytic reactor. The resulting ash is drained from the bottom of the carburetor.

In the case of the use of adsorption material with Ca content as by-products, stable salts and gypsum are formed, which are suitable for disposal.

The basic chemical reactions of absorption of S and C1 in the mentioned process are:

Ca (OH) ₂ (s) + H ₂ S (g) = CaS (s) + 2 H ₂ O (g) (2);

Ca (OH) ₂ (s) + HCl (g) = CaCl ₂ (s) + 2 H ₂ O (g) (2), where Ca (OH) ₂ can also replace CaO or CaCO ₃ .

Detailed description of the invention

The gasification process is shown in Figure 1 and is carried out by dosing carbon dioxide material 5 from the appropriate storage tanks into the mixer 1, optional additives (such as wood sawdust, sewage sludge or heavy municipal waste fraction) if necessary. and adsorbent 6 for binding S and Cl, and optionally water. The content of C1 and / or S in the gasification material 5 is determined by means of a preliminary analysis and subsequent assessment of the range of the contents of Cl and / or S.

Based on the determined content of Cl and / or S, the gasification material 5 is mixed with an appropriate amount of adsorbent 6. To achieve effective binding of S and Cl during gasification, said adsorbent 6 is dosed in stoichiometric excess so that the amount of adsorbent 6 dosed into gasification material 5 is 1.5 to 5 times, preferably 2.5 times its stoichiometric amount. Said excess of adsorbent 6 in the gasification material 5 enables a smooth process even if the Cl and / or S content in the gasification material 5 is higher than the Cl and / or S content determined by said preliminary analysis and subsequent evaluation. The unused adsorbent 6 behaves inertly in the process and does not affect the gasification process. The dosing of water into the mixer is optional and is only suitable in the case of very dry gasification material, because with a more moist material it is easier to achieve the appropriate density of the raw material, and dosing is also facilitated.

The gasification raw material thus prepared is transported from the mixer 1 to the gasifier 2, where a product gas is formed, which is fed to the catalytic reactor 3, where the present tars or hydrocarbons are converted into hydrogen and carbon monoxide and hot synthesis gas is obtained. The hot synthesis gas can then be used or passed through a heat exchanger with a dehumidifier 4, where the synthesis gas is cooled and condensate water 13 is removed.

The materials entering the process are a material with a carbon content of 5, an adsorbent 6, the amount of which is determined on the basis of the determined content of C1 and / or S, a first oxidant 7 and water or water vapor 8 fed to the carburetor 2, and a second oxidant 9 it is fed to the catalytic reactor 3.

The materials obtained from the process are ash 10, which is separated from the carburetor 2, hot synthesis gas 11, if it leaves the process before cooling, or condensate water 13 and cooled synthesis gas 14, which exit the cooling system with dehumidifier 4, as also excess heat 12.

The elimination process of components S and C1 is shown in Figure 2.

The prepared gasification raw material is metered or poured into the carburetor 2 so that the cold gasification material 15 moves from top to bottom, and the gas 16 formed by gasification of the gasification material 15 moves from bottom to top, ie countercurrently. This creates an upper cold filter layer of material 17, in which the material dries and cools due to the evaporation of water and compounds of Ca with S and CL are formed in said cold filter layer of material 17. Under layer 17 is a hot layer 18 in which pyrolysis, reduction and oxidation.

The integration of the processes of gasification, catalytic conversion and separation of components S and C1 is shown in Figure 3 and includes the following phases:

A. Preparation of the raw material for gasification, comprising the following steps:

i. dosing the gasification material 5 with carbon content into the mixer;

ii. in case of excessive granulation, grinding and mixing of the material from step (i);

iii. determining the C1 and / or S content of the gasification material 5, based on a preliminary analysis and subsequent assessment of the C1 and / or S content range;

iv. based on the determined content of C1 and / or S in the gasification material 5, dosing the adsorbent 6 into the gasification material 5, in a stoichiometric excess such that the amount of adsorbent 6 dosed into the gasification material 5 is from 1.5 to 3 times , preferably 2 times its stoichiometric amount. Said adsorbent 6 removes compounds C1 and / or S from the product gas in the gasification process;

v. mixing the gasification material 5 and the adsorbent 6;

you. optional pelleting of the resulting mixture; in vii. transport 19 of the obtained mixture or pelleted mixture, which is a pre-prepared raw material for gasification, to the carburetor 2;

B. Fuel gasification comprising the following steps:

i. dosing a first oxidant 7, such as air or oxygen and water or steam 8, into the lower part of the carburetor 2, below the grate 20;

ii. gasification of the fuel and reaching the maximum temperature in the hot layer 18, where the oxidation, reduction and pyrolysis process takes place, where said maximum temperature ranges between 600 ° C and 1,100 ° C, depending on the composition and properties of the gasification feedstock, especially moisture, where said temperature is lower in the case of a higher moisture content and higher in the case of a lower moisture content;

iii. removing compounds S and / or C1 and higher easily condensing tars, in a cold filter layer of material 17 having a high adsorption capacity;

iv. collecting the tar-containing product gas in the space 21 above said layer 17, where the product gas temperature is at least 120 ° C, and in case the product gas contains heavy tars, the product gas temperature is at least 300 ° C;

v. removal and transport 32 of ash 10 from the carburetor 2.

If necessary, the ash can be stabilized and disposed of as an inert material or used as a raw material, for example for the manufacture of building materials.

C. In the event that these compounds are not completely removed from the product gas during the gasification of materials containing compounds with S and Cl already in the gasification phase, one or more phase purification of the product gas 22 follows, where compounds S and / or Cl, which usually comprises the following steps:

i. hydrodesulfurization, which by hydrogenation of organic substances containing S and / or Cl, allows the removal of sulfur and / or chlorine by replacing hydrogen and S and / or Cl with hydrogen to form H2S and HCl;

ii. adsorption of HO by zeolites or other fillers;

iii. adsorption of H2S on ZnO or a similar alternative substance;

D. Conversion of tars into synthesis gas comprising the following steps:

i. feeding 23 the product gas purified of compounds S and / or Cl into the stirring part 25 of the catalytic reactor 3, where an appropriate amount of preheated second oxidant 9, such as air or oxygen, of the ignition gas 24, such as hydrogen, is added. and water or steam;

ii. mixing the product gas, the heated second oxidant 9 and the ignition gas present, in the stirring portion 25 of the catalytic reactor 3;

iii. ignition of the mixture from the previous step, in the ignition chamber 26 of the catalytic reactor 3, which is separated from the mixing part 25 by a flame barrier 27 and contains the ignition elements 28;

iv. conversion of tars into synthesis gas by partial oxidation and steam reforming of the mixture from the previous step in catalyst 29, catalytic reactor 3.

The operating temperature of the catalyst 29 is maintained by substoichiometric combustion of the product gas in the upper layers of the catalyst 29, where partial oxidation of the tars in the product gas (exothermic process) is preferably carried out, without generating complete oxidation products.

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 29.

In the case of too low tar concentrations, complete oxidation of part of the product gas can also be used to generate heat. The obtained heat heats the catalyst 29, where a steam conversion process takes place, which improves the calorific value of the synthesis gas at the outlet of the catalytic reactor.

The process described can be carried out with any type of gasifier, provided that the highest possible concentration of tar in the product gas is ensured, at least between 4 and 6 g / Nm, preferably at least 5 g / Nm, and an appropriate product gas temperature above the condensation limit of tars. , wherein said temperature depends on the type of tars present in the product gas and is at least 100 ° C, and in the case of the presence of more volatile tars said temperature of the product gas is at least 300 ° C.

E. Conducting 30 the synthesis gas from the catalytic reactor 3 to the first heat exchanger 31, which is the carburetor jacket 2, where the gas from the catalytic reactor 3 transfers part of the heat to the carburetor 2 and heats it. This reduces the need to add an oxidant to the gasification process, which is replaced by oxygen from the supplied water, and thus also increases the energy value of the product gas.

F. Conducting 33 the synthesis gas from the first heat exchanger 31 to the second heat exchanger 34. In the second heat exchanger 34, the synthesis gas emits part of the heat and thereby heats the second oxidant 9.

G. The conduction 35 of the partially cooled synthesis gas from the second heat exchanger 34 to the third heat exchanger 36, in which the synthesis gas emits part of the heat to the heat transfer medium 12, is cooled below the condensation temperature of the water and the moisture in the synthesis gas condenses. water on the dehumidifier (demister). Condensate extracted from the synthesis gas is usable as process water.

H. Conducting 14 cooled synthesis gas free of tar and dust particles from the described process to a storage tank or to devices for further use.

Refrigerated synthesis gas free of tar and particulate matter is useful as a technical gas, as an energy source for energy production or for the production of useful chemical products and gaseous or liquid fuels such as methane, methanol or other derivatives obtained, for example, from Fischer- Tropical process.

The process described is started automatically by heating the mixing part of the catalytic reactor to a temperature of 400 ° C with external heaters to avoid condensation of tars / hydrocarbons. The catalyst is heated to operating temperature by external electric heaters and / or external full combustion. After heating the catalyst and the mixing part of the catalytic reactor, the gasification material in the carburetor is ignited by blowing hot air onto the grate.

The process according to the present invention is characterized by:

a higher permissible concentration of tars in the product gas, which allows the gasification of low-quality or more complex materials with high moisture and / or dust contents, and thus the applicability of the gasification process is significantly extended; 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 allows the chemical reaction of the adsorbent with S and / or Cl, and thus the removal of S and / or C1 in gasification of materials containing S and / or Cl;

catalytic conversion of a higher tar product gas into synthesis gas;

partial tar oxidation process used for internal heating of a catalytic reactor, which allows autothermal catalytic conversion of tars by steam reforming without increasing inert components in the gas (eg N2 and CO2), while higher tar concentration linearly increases the H2 / CO ratio in synthesis gas;

the conversion of carbon into a gaseous state prior to the catalytic conversion, by a process of partial oxidation which results in the formation of no carbon or carbon black which would be separated into ash or into a product and / or synthesis gas;

lower emissions compared to incineration, and the fact that after gasification of the residue are inorganic ash which can be neutralized by additional thermal process and condensate water, which can be used as process water in the gasification process for dosing water into the material, or under the grate, in step B (i) described above, and for cooling the synthesis gas.

The process is useful for gasification of various types of materials. The result of the process is a synthesis gas, free of tars, compounds S and C1 and dust particles and with low concentrations of moisture, CH4 and CO2, in case it gives air as the first oxidant, as well as N2. Said synthetic gas is suitable for use as a raw material or energy source.

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

Claims (5)

Patent claims A process for the gasification of carbon-containing solid materials with a pronounced concentration of tars and their catalytic conversion to carbon monoxide and hydrogen, characterized in that it comprises the following stages: A. Preparation of the raw material for gasification, comprising the following steps: i. dosing the gasification material (5) with the carbon content into the mixer; ii. optional grinding and mixing of the material from step (i); iii. determining the content of C1 and / or S in the gasification material (5); iv. dosing a corresponding amount of adsorbent (6) into the gasification material (5); v. mixing the gasification material (5) and the adsorbent (6); you. optional pelleting of the resulting mixture; in vii. transport (19) of the mixture or pelleted mixture to the carburetor (2); B. Fuel gasification comprising the following steps: i. dosing a first oxidant (7), such as air or oxygen and water or water vapor (8) into the lower part of the carburetor (2), below the grate (20); ii. gasification of the fuel and reaching the maximum temperature in the hot layer (18); iii. removing compounds S and / or C1 and higher easily condensing tars, in a cold filter layer of material (17) having a high adsorption capacity; iv. collecting tar-containing product gas in a space (21) above said cold layer (17); C. Optional single or multi-phase purification (22) of the product gas, wherein the remaining compounds S and / or Cl are removed from the product gas, comprising the following steps: i. hydrodesulfurization; ii. HCl adsorption by zeolites or other fillers; iii. adsorption of H2S on ZnO or a similar alternative substance; D. Conversion of tars into synthesis gas comprising the following steps: i. feeding (23) the product gas purified of compounds S and / or Cl into the mixing part (25) of the catalytic reactor (3), where it is dosed with an appropriate amount of preheated second oxidant (9), ignition gas (24), such as hydrogen, and water or steam; ii. mixing the product gas, the heated second oxidant (9) and the ignition gas present, in the mixing part (25) of the catalytic reactor (3); iii. ignition of the mixture from the previous step, in the ignition chamber (26) of the catalytic reactor (3), which is separated from the mixing part (25) by a flame barrier (27) and contains ignition elements (28); iv. converting the tars into a synthesis gas by partial oxidation and steam reforming of the mixture from the previous step in the catalyst (29) of the catalytic reactor (3); E. Conducting (30) the synthesis gas from the catalytic reactor (3) to the first heat exchanger (31); F. Conducting (33) the synthesis gas from the first heat exchanger (31) to the second heat exchanger (34); G. Conducting (35) the synthesis gas from the second heat exchanger (34) to the third heat exchanger (36); H. Conducting (14) clean and cooled synthesis gas from the described process to a storage tank or to devices for further use. Process according to Claim 1, characterized in that: in step A, said step of determining the Cl and / or S content in the gasification material (5) takes place on the basis of a preliminary analysis and subsequent assessment of the range of Cl and / or S content in said material (5); - in step A, the amount of dosed adsorbent (6) is determined on the basis of the determined content of C1 and / or S in the gasification material (5), so that the amount of said adsorbent (6) is in stoichiometric excess and amounts to 1, 5 times to 5 times, preferably 2.5 times its stoichiometric amount, in phase B, the maximum temperature reached in the hot layer (18) ranges between 600 ° C and 1,100 ° C, depending on the composition and properties of the raw material for gasification. Process according to Claim 1 or 2, characterized in that: synthesis gas, in the first heat exchanger (31), which comes from the catalytic reactor (3), transfers part of the heat to the carburetor (2) and thus heats it; synthesis gas, in the second heat exchanger (34), where it comes from the first heat exchanger (31), transfers part of the heat to the second oxidant (9) and thereby heats it; synthesis gas, in the third heat exchanger (36), which comes from the second heat exchanger (34), part of the heat is transferred to the heat transfer medium (12), is therefore cooled below the condensation temperature of water, moisture in the synthesis gas condenses and is eliminated (13 ) as condensate water on the dehumidifier. Process according to any one of the preceding claims, characterized in that the materials leaving the process are: synthesis gas, free of tars, compounds S and C1 and dust particles and with low concentrations of moisture, CH4 and CO2, in case air is used as the first oxidant, as well as N2, where said synthetic gas is ready for further use; inorganic ash which, if necessary, is stabilized and disposed of as an inert material or used as a raw material, for example for the manufacture of building materials; in - process water used in the gasification process for dosing water into the gasification material or into the lower part of the carburetor (2), under the grate (20). Process according to any one of the preceding claims, characterized by: a higher permissible concentration of tars in the product gas, which allows the gasification of low-quality or more complex materials with high moisture and / or dust contents, and thus the applicability of the gasification process is significantly extended; 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 allows the chemical reaction of the adsorbent with S and / or Cl, and thus the removal of S and / or Cl in gasification of materials containing S and / or Cl; catalytic conversion of a tar gas with a higher tar content into synthesis gas, where partial tar oxidation is used as the main heat source for heating the catalytic reactor and therefore requires a sufficiently high concentration of tars in the product gas; the partial tar oxidation process used for internal heating of the catalytic reactor, followed by a catalytic steam reforming process and consequently linearly increasing the H2 / CO ratio in the synthesis gas, which depends on the previous tar content in the product gas; the conversion of carbon into a gaseous state prior to the catalytic conversion, by a process of partial oxidation which results in the formation of no carbon or carbon black which would be separated into ash or into a product and / or synthesis gas; lower emissions to the environment compared to incineration, and residues after gasification are inorganic ash and condensate water, which is used as process water in the process itself.