WO2020145904A1

WO2020145904A1 - Process for gasification of solid carbonaceous materials with a pronounced concentration of tars and their catalytic conversion into carbon monoxide and hydrogen

Info

Publication number: WO2020145904A1
Application number: PCT/SI2020/000002
Authority: WO
Inventors: Teos PERNE; Tine SELJAK; Marko ŠETINC
Original assignee: Perne Teos
Priority date: 2019-01-07
Filing date: 2020-01-06
Publication date: 2020-07-16
Also published as: SI25770A

Abstract

The present invention discloses a process for gasification of solid carbonaceous materials with a pronounced concentration of tars and their catalytic transformation into carbon monoxide and hydrogen, comprising the preparation of a gasification raw material including the dosage of gasification material, optional additives, adsorbent and water, gasification of the said raw material, optional mono- or multi-phase purification of product gas, transformation of tars into synthesis gas and leading the synthesis gas through a series of heat exchangers and a demister. The process allows a higher permissible tar concentration in the product gas, which enables the auto-thermal process of catalytic transformation and at the same time gasification of low-quality or more complex materials with high moisture and/or dust content, and thus the usefulness of the gasification process is significantly extended. The result of the process is a synthesis gas without tars, S and C1 compounds and dust particles and with low concentrations of moisture, CH₄ in CO₂, in the case when air is used as the first oxidant, also N₂. The said synthesis gas is suitable for use as a raw material or energy source. The residues after gasification are inorganic ash and condensed water, which is used as the process water in the process itself.

Description

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

Field of the invention:

Subject of the invention is the process of gasification of carbonaceous materials, for the production of pure synthesis gas without tar content.

Description of a technical problem :

The tar content in the production gas is still today a major problem in all gasification systems designed for production of combustible synthesis gas. There are several tar reduction measures that can be classified as:

- primary measures (measures within the gasifier) that rely on appropriate control strategies or maintenance of the conditions of the gasification process and the current dynamics in the gasifier to minimize the tar formation. Because of this, technological solutions limit the operation in terms of system flexibility, the possibilities of different device dimensions; in addition the devices are extremely limited in the selection and preparation of gasification materials, while they may produce a large amount of charcoal as a by-product and operate under very limited operating conditions. Although primary measures can significantly reduce the tar content, it is practically impossible to completely remove tars without the use of secondary measures.

- secondary measures (the measures after the gasifier) relying on the after-treatment of product gas by various methods (thermal cracking, catalytic conversion, washing). Such measures also have certain disadvantages: they are not enough efficient, they are too expensive, they negatively affect the heating value of the gas or they shift the tar problem to wastewater treatment. In the case of catalytic secondary measures, the energy for endothermic processes is in most cases obtained from an external heat source (with feeding of hot gas or electric heaters). Within the limits of thermodynamic capabilities, all the existing gasification processes are currently adjusted and optimized for the production of product gas with as low as possible tar content, since this causes technical problems in gasification systems and subsequent applications. The tar content of product (synthesis) gas ranges from 0.1% (downdraft gasifier; i.e. co-current fix bed gasifier) to 20% (updraft gasifier; i.e. counter-current fix bed gasifier) or more (in pure pyrolysis processes). The energy value of the product (synthesis) gas ranges from 5 MJ/Nm³ to 15 MJ/Nm³ and is considered to be low- or medium-caloric gas compared to natural gas (35 MJ/Nm³). If air is used as the oxidant, the product (synthesis) gas contains about half of N2. The relative amount of CO, CO2, H2O, ¾ and hydrocarbons depends on the stoichiometry of the gasification process. The air/gasification material ratio in the gasification process is generally in the range of 0.2 - 0.35, but if steam is used as the oxidant, the vapor/gasification material ratio is about 1. The actual amount of CO, CO2, ¾0, ¾, tar or hydrocarbons depends on the partial oxidation of the volatile hydrocarbons shown by the following equation: C_nH_m + (n/2 + m/4) 0_{2 n}CO + (m 2) H₂0.

Usually, the materials, as homogeneous and dry as possible, that are properly treated and purified are used in gasification processes with aim to minimize the tar content in the product (synthesis) gas, and in particular it is avoided the use of materials containing substances with elements S and Cl. The problem of the presence of S and also Cl 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 resolved outside the thermal conversion process, after it, by the washing of product or flue gas (together with other secondary tar removal measures) or before it, by removing substances with S and Cl content from the thermal conversion input materials. There are also known methods of removing S and Cl during the thermal combustion process itself, particularly 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 to extract as much as possible S and Cl into the ash already in the burning process. State of the art

The tar gasification and transformation process is described in patent US 8,936,886 B2, according to which the fuel is dosed into an updraft gasifier in which the process conditions are optimized for production of product gas with the lowest tar concentration possible. The tars, formed despite of that, are then transformed in the next phase by a thermal cracking process. Optimizing the production of product (synthesis) gas with as little tars as possible limits the use of heterogeneous and moist raw materials, and the use of thermal cracking significantly reduces the energy value of the synthesis gas.

Methods for removing elements S and Cl by adding an absorbent to the fuel are already described in patents US 174.348, EP 1765962, US 6.599.123 and US 5.571.490. All of the indicated examples describe the use of additives in the burning process, which is a rapid chemical reaction, with large temperature gradients, when the fuel is very quickly dried, gasified and completely oxidized. In the described conditions of rapid reaction or very high temperatures, the other chemical reactions do not have sufficient time to proceed optimally, since the retention times are extremely short, especially when compared to gasification, where the drying and gasification reactions take place in a time span of few seconds. As a result, the effects of bonding S and Cl with, for example, Ca or Mg into solid compounds are significantly more effective in gasification, so that virtually all S and Cl can be removed as early as the gasification phase with ash.

A possible integrated solution of the gasification process using a catalyst for the tar transformation, while also the process of removing the S and Cl elements by adding an adsorbent is taking place, is presented in patent EP 0512305, which describes the use of RDF raw material (recovered municipal waste) for gasification. A fluidized bed gasifier is used. Catalytic conversion and removal processes of S and Cl are also carried out in a fluidized bed, where a dust mixture of limestone, dolomite and alkaline adsorbent is added to the gas stream, circulating all the time throughout the system. However, the product gas is laden with ash and, after catalytic reactions, needs to be cleaned with particulate separators, water showers and filters. The fuel must be properly prepared or broken 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 the description of present invention, "product gas" is gas coming from a gasifier to a catalytic reactor where it is converted into "synthesis gas".

the essential difference between the product gas and the synthesis gas is that the product gas contains tars and dust particles, while the synthesis gas consists predominantly of partial oxidation products (CO and ¾) and inert components that depend on the oxidant used, and in particular and it is without tar and dust particles and does not need to be further purified before further use for the synthesis of raw materials or as a fuel.

Furthermore, the term "pure synthesis gas free of water or moisture" means a gas mixture which is without moisture and consists of CO, !¾, and additionally CO2, CH4 and a minimum of moisture content.

Short description of accompanying figures:

The present invention is described below by means of the accompanying figures showing:

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

Figure 2: schematic illustration of the process of the extraction of S and Cl components;

Figure 3: schematic illustration of the integration of the gasification process, the catalytic conversion and the extraction of the S and Cl components.

Description of the invention

The present invention solves the problem of the presence of tar arising from the gasification of carbonaceous materials by adjusting the conditions of gasification to emphasizing formation of tars or hydrocarbons in the product gas, where these increased concentrations of tars (or hydrocarbons) represent the optimal entry reactant for the operation of catalytic conversion of product gas into the synthesis gas that takes place in the catalytic reactor. The described process can be carried out with any type of gasifier, provided that a minimum tar concentration in the product gas of at least 4 g/Nm³ to 6 g/Nm³, preferably at least 5 g/Nm³, is provided, as well as an adequate exit temperature of the product gas obtained 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. Updraft gasifiers of all kinds are particularly suitable for gasification in the described method. Any catalyst designed for transformation of hydrocarbons into hydrogen and carbon monoxide may be used for transformation of tars or hydrocarbons in a catalytic reactor. This simplifies the process conditions of gasification, which are much more manageable, and extends the range of raw materials used for gasification to those in which the heterogeneity of composition and moisture is desirable. For the operation of catalytic reactor, the presence of higher hydrocarbon concentrations means more optimal process conditions, which significantly improves the conditions for the transformation of all hydrocarbons to hydrogen and carbon monoxide and thus a pure synthesis gas.

An essential feature of the process according to the present invention and thus a significant difference from all such processes according to the state of the art is that the heterogeneity of the gasification material as well as the presence of moisture in the gasification material is desirable and also that in the gasification process are purposely produced higher tar concentrations, which are crucial for the auto-thermal course of catalytic tar conversion without increasing the inert components in the resulting gas (e.g. N2 and CO2). This is achieved by feeding or by the presence of water or water vapor, which plays a key role in the process:

- water present in the gasification material lowers by evaporation the gasification temperature in the gasifier in the upper layers and facilitates processes in which more tars are formed and simultaneously supports the processes of binding S and/or Cl with the adsorbent;

- water or water vapor dosed under the gasifier grid lowers the temperature in the lower layers and supplies additional oxygen and hydrogen to the process;

- water vapor, which during drying and pyrolysis process evaporates and is an integral part of product gas, enriches the synthesis gas with additional hydrogen in the catalytic conversion with steam reforming. In order to generate thermal energy in the gasification process, primarily, a partial oxidation of carbonaceous materials to CO and in minimal possible extent an oxidation of the materials into carbon dioxide, CO2 are taking place. Under the oxidation zone, in addition to the oxidant, also water or water vapor is fed, which regulates the gasification temperature, and especially water vapor represents an additional source of hydrogen in the case of gasification of carbonaceous materials from less volatile compounds, such as coals, so that sufficiently high concentrations of hydrocarbons in the product gas can be formed also from such materials. A small amount of oxidant is then added to the product gas which is led to a catalytic reactor, where a catalytic reaction of partial oxidation and also steam reforming is taking place using the catalyst by which the tars are decomposed into CO and ¾. The process in the gasifier and in the catalytic reactor is led so that it is auto-thermal.

The present invention also solves the extraction of S and Cl components already within the gasification process. A raw material with an adequate moisture content must be used and the process must be led at lower temperatures and with longer retention times in the drying and pyrolysis phases, which, when the adsorbent is added, makes extremely efficient binding of elements S and Cl with the adsorption material (containing e.g. Ca or Mg) and their extraction into ash. Thereby, the range of materials suitable for gasification is also extended to the area of municipal and other waste or materials which are suitable for gasification and which may contain substances containing S and Cl. Extension of the range of useful gasification materials is achieved by adding an adsorption material which under conditions of gasification of the wet material binds the sulphur and chlorine already in the gasifier, namely into such compounds which are already in the gasifier extracted in solid form into ash to prevent the formation of the gaseous compounds with elements S and Cl and their passage to a catalytic reactor. The resulting ash is discharged from the bottom of the gasifier.

In the case of using adsorption material with Ca content, stable salts and gypsum are formed as stable by-products which are safe to deposit.

The basic chemical reactions of S and Cl absorption in the said process are:

Ca(OH)₂(s) + ¾S(g) = CaS(s) + 2 H₂0(g) (2); Ca(OH)2(s) + HCl(g) = CaCl2(s) + 2 H₂0(g) (2), where Ca(OH)2 may also be replaced by CaO or CaC(>3.

Detailed description of the invention

The gasification process is shown in Figure 1 , and is carried out by feeding the carbonaceous material 5 for the gasification, optional additives (such as wood sawdust, sewage sludge or heavy fraction from municipal waste) as needed, and adsorbent 6 for the binding of S and Cl, and water as needed from the appropriate storage tanks into the mixer 1. The content of Cl and/or S in the gasification material 5 is determined by preliminary analysis and subsequent assessment of the range of Cl and/or S content. Based on the determined Cl and/or S content, a suitable amount of adsorbent 6 is added to the gasification material 5. To achieve effective binding of S and Cl during gasification, the said adsorbent 6 is dosed in stoichiometric excess so that the amount of adsorbent 6 dosed into the gasification material 5 is 1.5 times to 5 times, preferably 2.5 times greater than its stoichiometric quantities. The said excess of adsorbent 6 added to the gasification material 5 enables the process to proceed smoothly even if the content of Cl and or S in the gasification material 5 is higher than the content of Cl and / or S determined by the aforementioned preliminary analysis and subsequent evaluation. The adsorbent 6 unused in the process behaves inertly and does not affect the gasification process. Feeding of water into the mixer is optional and is only appropriate in the case of very dry gasification material, since the wetter material makes it easier to obtain the proper density of the raw material and also facilitates dosing.

The gasification raw material thus prepared is conveyed from the mixer 1 to the gasifier 2, where a product gas is produced, which is fed into the catalytic reactor 3, where the tars or hydrocarbons present are converted to hydrogen and carbon monoxide, thus forming a hot synthesis gas. The hot synthesis gas can then be used or run through a heat exchanger with a demister 4, where the synthesis gas is cooled and condensed water 13 is extracted.

The input materials for the process are carbonaceous material 5, adsorbent 6, the amount of which is determined on the basis of the determined Cl and/or S content, the first oxidant 7 and the water or water vapor 8 fed into the gasifier 2, and the second oxidant 9 which it is fed into the catalytic reactor 3.

The materials obtained from the process are ash 10, which is extracted from the gasifier 2, hot synthesis gas 11, if it exits the process before cooling, or condensed water 13 and cooled synthesis gas 14, which exit the cooling system with a demister 4, as also excess heat 12.

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

The prepared gasification raw material is fed or poured into the gasifier 2 so that the cold gasification material 15 moves from the top down and the gas 16 formed by the gasification of the gasification material 15 moves from the bottom up, i.e. counter- current. This creates an upper cold filter layer of material 17, in which the material is dried and cooled due to the evaporation of water and the Ca compounds with S and Cl are formed in the said cold filter layer of material 17. Under layer 17 is a hot layer 18 in which pyrolysis, reduction and oxidation take place.

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

A. Preparation of the gasification raw material, comprising the following steps: i. dosing of the carbonaceous material 5 for gasification content into the mixer;

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

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

iv. dosing of adsorbent 6 into gasification material 5 in stoichiometric excess, based on the determined Cl and/or S content in the gasification material 5, so that the amount of adsorbent 6 dosed into the gasification material 5 is 1.5 times to 3 times, preferably 2 times greater than its stoichiometric quantities. The said adsorbent 6 removes Cl and/or S compounds from the product gas in the gasification process; v. mixing gasification material 5 and adsorbent 6;

vi. optional pelleting of the resulting mixture; and

vii. conveying the resulting mixture or pelleted mixture, which represent a pre-prepared gasification raw material, into the gasifier 2;

B. Gasification of the fuel comprising the following steps:

i. dosing the first oxidant 7, such as air or oxygen, and water or vapor 8 into the lower part of the gasifier 2, below the grid 20;

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

iii. removing S and/or Cl compounds and higher easily condensing tars in the cold filter layer of material 17 having a high adsorption capacity; iv. collecting tar-containing product gas in the space 21 above the said layer 17, where the product gas temperature is at least 120 °C, and if the product gas contains heavy tars, the temperature of the product gas is at least 300 °C;

v. removing and conveying 32 the ash 10 from the gasifier 2.

The ash can be stabilized as needed and deposited as an inert material or used as a raw material, for example for the manufacture of construction materials.

C. If during the gasification of the materials containing the compounds with S and Cl the said compounds are not completely removed from the product gas already in the gasification phase, the mono- or multi-phase pre-treatment of the product gas 22 follows, where the S and/or Cl compounds are removed from the product gas, which usually involves the following steps: i. hydrodesulphurization which, by hydrogenation of organic substances containing S and/or Cl, enables the removal of sulphur and/or chlorine by the replacement of S and/or Cl with hydrogen to produce ¾S and HC1;

ii. adsorption of HC1 taking place by the use of zeolites or other fillers; iii. adsorption of ¾S taking place on ZnO or on a similar alternative substance;

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

i. feeding 23 the product gas purified of S and/or Cl compounds into the mixing part 25 of catalytic reactor 3, where we add to it an appropriate amount of pre-heated second oxidant 9, such as air or oxygen, of the ignition gas 24, such as hydrogen, and water or water vapor; ii. mixing product gas, heated second oxidant 9 and present ignition gas in the mixing part 25 of the catalytic reactor 3;

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

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

The operating temperature of the catalyst 29 is maintained by sub-stoichiometric combustion of product gas in the upper layers of the catalyst 29, where partial oxidation of tars in the product gas (exothermic process) takes place without generating products of complete oxidation.

Homogeneous post-stoichiometric 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 Cio¾ consumed during partial oxidation for achieving 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. Obtained heat heats the catalyst 29, where a process of steam transformation also takes place to improve the calorific value of the synthesis gas at the outlet of the catalytic reactor.

The described process can be carried out with any type of gasifier, provided that the formation of a maximum tar concentration in the product gas is provided at least between 4 and 6 g/Nm³, preferably at least 5 g/Nm³, and an appropriate product gas temperature above the tar condensation limit, where the said temperature depends on the type of tar contained in the product gas, and amounts at least to 100 °C, and in the case of presence of the tars, which are more difficult to vaporize, the said product gas temperature is at least 300 °C.

E. Feeding 30 of the synthesis gas from the catalytic reactor 3 to the first heat exchanger 31 , which is the double wall housing of the gasifier 2, where the gas from the catalytic reactor 3 emits part of the heat to the gasifier 2 and heats it. This reduces the need for the oxidant to be fed into the gasification process, which is replaced by oxygen from the supplied water, thereby increasing the energy value of the product gas.

F. Feeding 33 of 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 a part of the heat, thereby heating the second oxidant 9.

G. Feeding 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 a part of the heat to the heat transfer medium 12, is cooled to a temperature of water condensation and the moisture in the synthesis gas condenses and is extracted 13 as condensation water at demister. Condensed water extracted from synthesis gas is useful as process water.

H. Feeding 14 of the cooled synthesis gas without tars and dust from the described process into the storage tank or to devices for further usage. Cooled synthesis gas without tars and dust particles 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, with Fischer-Tropsch process.

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

The process according to the present invention is characterized by:

- higher permissible tar concentration in the product gas, which allows gasification of low-quality or more complex materials with high moisture and/or dust content, and thus the usefulness of the gasification process is significantly extended;

slow gasification of materials at lower temperatures in the presence of moisture and proper filling of material, which creates a filter (adsorption) zone and allows chemical reaction of the adsorbent with S and/or Cl, thereby removing S and/or Cl in gasification of materials which contain S and/or Cl;

catalytic transformation of product gas with higher tar content to synthesis gas;

- process of partial tar oxidation used for the internal heating of a catalytic reactor that allows the auto-thermal course of catalytic tar transformation by steam reforming without increasing the inert components in the gas (e.g. N2 in CO2), while the increased tar concentration linearly increases the H2/CO ratio in synthesis gas;

transformation of carbon to a gaseous state prior to catalytic transformation, by a partial oxidation process, which does not result in the formation of charcoal or soot which would be extracted into ash or into product and/or synthesis gas; lower emissions compared to incineration, and that after the gasification, the residues are inorganic ash which can be neutralized, if needed, by additional thermal process, and condensed water, which is useful as process water in the gasification process itself for dosing water into the material or under the grid in step B(i) described above and for cooling the synthesis gas.

The process is useful for gasification of different types of materials. The result of the process is a synthesis gas, free of tars, S and Cl compounds and dust particles and with low concentrations of moisture, CH₄ and CO₂ and when air is used as the first oxidant also N₂. The said synthesis gas is suitable for use as a raw material or energy source.

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

Claims

1. Process of gasification of solid carbonaceous materials with a pronounced concentration of tars and their catalytic conversion into carbon monoxide and hydrogen, characterized by comprising the following phases:

A. Preparation of the gasification raw material, comprising the following steps: i. dosing of gasification material (5) with carbon content into the mixer; ii. optional grinding and mixing of the material from step (i);

iii. determining the Cl and/or S content in the gasification material (5); iv. dosing the corresponding amount of adsorbent (6) into the gasification material (5);

v. mixing gasification material (5) and adsorbent(6);

vi. optional pelleting of the resulting mixture; and

vii. conveying (19) the mixture or pelleted mixture to the gasifier (2);

B. Gasification of the fuel comprising the following steps:

i. dosing the first oxidant (7), such as air or oxygen, and water or water vapor (8) into the lower part of the gasifier (2), below the grid (20); ii. gasification of the fuel and reaching the maximum temperature in the hot layer (18);

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

iv. collecting tar-containing product gas in a space (21) above the said cold layer (17);

C. Optional mono- or multi -phase pre-treatment of the product gas (22), where the remaining S and/or Cl compounds are removed from the product gas, which involves the following steps:

i. hydrodesulphurization;

D. The conversion of tars into synthesis gas comprising the following steps: i. feeding (23) the product gas purified of S and/or Cl compounds into the mixing part (25) of catalytic reactor (3), where we add to it an appropriate amount of pre-heated second oxidant (9), of the ignition gas (24), such as hydrogen, and water or water vapor; ii. mixing product gas, heated second oxidant (9) and present ignition gas in the mixing part (25) of the catalytic reactor (3); iii. ignition of the mixture from the preceding step in the ignition

chamber (26) of the catalytic reactor (3), which is separated from the mixing part (25) by a flame arrester (27) and contains ignition elements (28);

iv. the transformation of tars into the 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. Feeding (30) of the synthesis gas from the catalytic reactor (3) to the first heat exchanger (31);

F. Feeding (33) of the synthesis gas from the first heat exchanger (31) to the second heat exchanger (34);

G. Feeding (35) of the synthesis gas from the second heat exchanger (34) to the third heat exchanger (36);

H. Feeding (14) of the purified and cooled synthesis gas from the described process into the storage tank or to devices for further usage.

2. Process according to claim 1, characterized in that:

- in phase A, the said step of establishing the Cl and/or S content in the gasification material (5) is taking place based on a preliminary analysis and subsequent assessment of the range of Cl and/or S content in the said material (5);

in phase A, the amount of dosed adsorbent (6) is determined based on the established content of Cl and/or S in the gasification material (5), namely in such way that the amount of said adsorbent (6) is in stoichiometric excess and amounts from 1.5 up to 5 times, preferably 2.5 times its stoichiometric quantity; 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 gasification raw material.

3. Process according to claim 1 or 2, characterized in that:

synthesis gas in the first heat exchanger (31), to which it flows from the catalytic reactor (3), emits part of the heat to the gasifier (2), thereby heating it;

- synthesis gas in the second heat exchanger (34), to which it flows from the first heat exchanger (31), emits part of the heat to the second oxidant (9), thereby heating it;

synthesis gas in the third heat exchanger (36), to which it flows from the second heat exchanger (34), emits part of the heat to the heat transfer medium (12) and is thus cooled below the water condensation temperature, the moisture in the synthesis gas condenses and is extracted (13) as condensed water on the demister.

4. Process according to any of the preceding claims, characterized in that the exiting materials are:

- synthesis gas, free of tars, S and Cl compounds and dust particles and with low concentrations of moisture, CH4 in CO2, in the case when air is used as the first oxidant, also N2, where the said synthesis gas is ready for further use;

- inorganic ash is stabilized as needed and deposited as an inert material or used as a raw material, for example for the manufacture of construction materials; and

- process water used in the gasification process itself for dosing water into the gasification material or into the lower part of the gasifier (2), below the grid (20).

5. Process according to any of the preceding claims, characterized by: higher permissible tar concentration in the product gas, which allows gasification of low-quality or more complex materials with high moisture and/or dust content, and thus the usefulness of the gasification process is significantly extended;

- catalytic transformation of product gas with 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 tar concentration in the product gas;

- the process of partial tar oxidation used for the internal heating of the catalytic reactor, followed by the catalytic process of steam reforming and consequently linear increasing of the H₂/CO ratio in the synthesis gas, which depends on the previous tar content in the product gas;

the transformation of carbon to a gaseous state prior to catalytic transformation, by a partial oxidation process, which does not result in the formation of charcoal or soot which would be extracted into ash or into product and/or synthesis gas;

- lower emissions into environment compared to incineration and the residues after gasification are inorganic ash and condensed water, which is used as process water in the process itself.