EP4023736A1

EP4023736A1 - Gasification device for the valorization of substances contained in a carbonaceous feedstock material

Info

Publication number: EP4023736A1
Application number: EP21218275.2A
Authority: EP
Inventors: Vittorio DELL'ACQUA
Original assignee: Sites Impianti Termici Elettrici E Strumentali Srl Soc
Current assignee: Sites Impianti Termici Elettrici E Strumentali Srl Soc
Priority date: 2020-12-31
Filing date: 2021-12-30
Publication date: 2022-07-06
Also published as: IT202000032942A1

Abstract

Gasification device (10) for the valorization of substances contained in a carbonaceous feedstock material, said device comprising a reactor body (11) in which a first and a second end (11a, 11b) are defined, said reactor body being provided with a corresponding inlet (13) for said feedstock material (Fs) to be treated and with at least a first inlet (15) for introducing feed gases (G1, G2) into said body (11), wherein said device is configured to perform at least two treatment stages (S1, S2) for the gasification of said feedstock material (Fs) in order to obtain a syngas (Gu), wherein said device (10) further comprises: a gas distribution system (19) associated with said first inlet (15) in order to distribute the feed gases (Gl, G2) inside the body (11) and comprising in turn mixing means (27) for mixing said gases (Gl, G2) with said feedstock material (Fs) in order to obtain a first gasification of said feedstock material (Fs) in a first treatment stage (SI); first dissociation means (39) comprising first grids (39) and first heat storage means (47) and second dissociation means (53) comprising second grids (53) and second heat storage means (61) for performing a treatment of gasification of the molecules of the feedstock material (Fs) that have not been gasified in the first treatment stage (S1); a purification system (63) for separating the gaseous fraction obtained from said treatment stages (S1, S2) from ashes; and wherein said gas distribution system (19), said first and second dissociation means (39, 53) and said purification system (63) are arranged in cascade from the first to the second end (11a, 11b) of the body (11) in order to promote a process of co-current gasification.

Description

Technical Field

The present invention relates to a gasification device for the valorization of substances contained in a carbonaceous feedstock material, i.e. a carbon-containing feedstock material. More particularly, the invention relates to a co-current or "downdraft", gasification device, in which the gasification process takes place from top downwards, by exploiting the force of gravity.

Prior Art

In the field of so-called renewable energies, chemical processes such as, for example, gasification processes are known, allowing conversion of a carbon-rich feedstock material into carbon monoxide, hydrogen and other gaseous compounds. The gasification process takes place by thermal degradation and usually provides for reaching high temperatures, preferably higher than 700-800 °C, in the presence of an under-stoichiometric percentage of an oxidizing agent, typically air (oxygen) or vapor. The resulting gaseous mixture is what is referred to as synthesis gas ("syngas") and is per se a fuel.
The gasification process is also a way to obtain energy from different types of organic materials and finds application also in the heat treatment of waste. In this respect, gasification devices, or gasifiers, are known using a feedstock material of organic type in order to obtain gaseous fuels than can be used for energy production.
Gasifiers exploit molecular dissociation, by means of pyrolysis process, said molecular dissociation being used for direct conversion of organic materials into gases, by heating, in the presence of small amounts of oxygen. The organic materials become fully destroyed as a result of the dissociation of their molecules, usually consisting of long carbonaceous chains, into simpler molecules of carbon monoxide, hydrogen and methane, which form a "synthesis gas" ("syngas"). Syngas is a combustible gas consisting largely of methane and carbon monoxide. Other products of gasification are "char", a carbonaceous solid, very similar to coal, and "tar", a liquid detrimental to installations and consisting of aromatic hydrocarbons of a tarry type, carbon dioxide and nanoparticulates. The environmental impact of a gasifier increases as the percentage of tar in the syngas increases. The presence of tar in the syngas depends on several factors, such as the combustion temperature, the pressure in the reactor where the molecular dissociation reaction takes place and the type of fuel used.
The more widespread applications of gasifiers relate to specific types of waste, such as, for example, paper mill waste, tires, plastics, biomass (vegetable waste, wood, olive pomace, etc.).
Many different solutions of gasification devices that can treat many different types of waste are known in the field. However, current gasification devices have a structure and operating principle that vary according to the type of waste to be treated. In most cases, it is not possible to use a single gasification device to treat waste regardless of its type.
In the context of increasing the contribution of renewable energy, there is therefore a strong need for a gasification device capable of processing a multitude of feedstock materials, of the organic type, in order to obtain gaseous fuels, or so-called synthesis gases, which can subsequently undergo various treatments to obtain pure gaseous hydrogen, liquid carbon dioxide and liquid methane.
The main object of the present invention is therefore to overcome the drawbacks of pior art by providing a gasification device for the valorization of substances contained in a feedstock material, irrespective of the nature of such feedstock material.
A further object of the invention is to provide a gasification device that can be used autonomously, or that can be associated downstream of digestion plants, or plants for the dehydration of the feedstock material treated by said device, or that can be associated upstream of known plants intended for treating the syngas obtained in said device, in order to produce liquid carbon dioxide, liquid methane or gaseous hydrogen.
Not least object of the invention is to provide a gasification device that can be manufactured industrially in a cost-effective manner.
These and other objects are achieved by the gasification device as claimed in the appended claims.

Summary of the Invention

The gasification device according to the invention allows carrying out a gasification process, or molecular dissociation process, of a carbonaceous feedstock material, in order to valorize the substances contained therein. The feedstock material used can be selected from a multitude of waste types, such as, for example, paper mill waste, tires, plastics, biomass (vegetable waste, wood, olive pomace, etc.), USWOF, possibly pre-treated, or digestate coming from digestion plants.
The gasification device relates to a co-current or downdraft process, in which the gasification process takes place from top to bottom of the device, when the device is in its operating configuration, by exploiting the force of gravity.
In addition, the gasification device according to the invention may be fed with a certain amount of feedstock material and can thus operate autonomously to obtain a syngas as a result of the gasification process. Alternatively, the gasification device according to the invention can be arranged downstream of sludge digestion or dehydration plants, or upstream of suitable dedicated plants intended for producing carbon dioxide, gaseous hydrogen or methane from the syngas produced by said device.
The gasification device comprises a reactor provided with a corresponding inlet for a certain amount of feedstock material to be treated and with at least a first inlet for introducing feed gases allowing carrying out the gasification process, said inlets being arranged at a first end of the device. Preferably, the feed gases are selected from carbon dioxide CO₂, oxygen O₂ and water H₂O in the form of vapor.
The gasification device is adapted to perform at least two treatment stages, namely a first treatment stage for the gasification of the solid fraction of the feedstock material to be treated by mixing it with certain feed gases introduced into the device, and a second treatment stage of dissociation of the gaseous fraction obtained at the first treatment stage.
Furthermore, still at the first treatment stage, a first dissociation of the complex gaseous molecules into simple molecules obtained from the transformation of the solid fraction into gaseous phase takes place. Preferably, the temperature inside the reactor at this first stage is between 700°C and 800°C, more preferably the temperature is 750°C.
The gasification device comprises a check valve for varying the thickness of the layer of the solid fraction of feedstock material entering the reactor. Preferably, the check valve is a gate valve, more preferably a knife gate valve, made of steel and having adjustable frequency in order to vary the thickness of the solid fraction.
Considering that the gasification process is a co-current process, the body of the gasification device is a vertical axis reactor, more preferably having a cylindrical shape.
The gasification device further comprises a gas distribution system, associated with the first inlet provided for the feed gases, in order to distribute the gases inside the reactor.
Preferably, both the first inlet and the system for distributing the gases inside the reactor are arranged near the upper end, or first end, of the reactor.
The gas distribution system comprises mixing means for mixing the feed gases with the solid fraction of the feedstock material treated at the first treatment stage.
In addition, the gasification device comprises first dissociation means and second dissociation means to perform a treatment of gasification of the molecules of the solid fraction that have not been gasified yet.
The gasification device further comprises a system of purification of the gases exiting the second treatment stage, for separating the gases from the ashes that are formed during the gasification process.
Advantageously, the gas distribution system, the first dissociation means, the second dissociation means and the gas purification system are arranged in cascade from top to bottom of the device, when said device is in its operating condition, in order to promote a process of co-current gasification.
Preferably, the gas distribution system comprises at least one movable, especially rotary, agitator or mixer, driven by a corresponding electric motor and equipped with mixing means adapted to mix the gases with the solid fraction of the feedstock material entering the reactor. More preferably, the mixing means comprise a plurality of first arms, distributed in an axial direction on the body of the agitator or mixer and extending radially relative to the body of the agitator or mixer.
Advantageously, the first arms of the movable agitator are arranged in a sunburst pattern, offset relative to one another in order to define a plurality of reaction layers associated with the first inlet provided for the feed gases. Preferably, the first arms and the body of the agitator are hollow in order to allow the gases to flow thereinto.
The gas distribution system further comprises a plurality of second, stationary arms arranged at different levels, each level being provided with a corresponding inlet for the feed gases. Preferably, the second, stationary arms are arranged offset relative to the first arms of the movable agitator.
Preferably, the percentages of the gases entering the reactor vary according to the temperature and the reaction to be obtained in each reaction layer. More preferably, in at least one of the reaction layers, the reaction C + CO₂ = 2CO is promoted, allowing an increase in the porosity of the residual carbon of the solid fraction, in order to obtain a catalyst for the dissociation of the complex gaseous molecules deriving from the mixing carried out by the agitator.
Preferably, the percentages of the gases entering the movable agitator, in particular entering the first arms, will be uniform and vary depending on the feedstock material treated by the reactor.
In addition, each arm of the movable agitator is preferably inclined relative to a corresponding transverse plane, perpendicular to the body of the agitator, for facilitating traveling of the solid fraction downwards.
The first, movable arms and the second, stationary arms of the agitator further comprise openings for the exit of gases. Preferably, the openings are oriented downwards, i.e. towards the lower end, or second end, of the rector.
The agitator or mixer further comprises means for adjusting the rotation speed in order to prevent areas of accumulation of the solid fraction and obtain an optimal mixture from the mixing of the solid fraction with the feed gases for the reactor.
Preferably, the first dissociation means are arranged under the gas distribution system and are adapted to break the carbonaceous particles of the solid fraction that have not been gasified yet.
Preferably, the first dissociation means comprise first grids comprising at least one mobile grid and one fixed grid. More preferably, the fixed grid has a mesh size of about 5 mm and is surmounted by first heat storage means comprising a plurality of first spherical beads, preferably made of metal, for example iron, having a diameter between 25 mm and 35 mm, more preferably a diameter of 30 mm, for allowing passage of particles smaller than 5 mm. The mobile grid is adapted to break the carbonaceous particles of the solid fraction that have not been gasified yet, by moving the first spherical beads at predetermined time intervals, in order to obtain dissociation of the carbonaceous particles having a size larger than 5 mm. Preferably, the first spherical beads are arranged in layers on the fixed grid. More preferably, the overall thickness of the layers of first spherical beads is sized so as to obtain, as a result of the movement of the mobile grid, stirring and breakage of the carbonaceous matter, and even more preferably, said thickness is between 50 mm and 70 mm.
At the second treatment stage of the gasification device, the dissociation of the residual chains deriving from the first treatment stage takes place in the presence of catalyst elements, such as for example the carbon particles exiting the first grids. Preferably, the reaction temperature at this second treatment stage is between 800°C and 900°C, more preferably of about 850°C.
In order to carry out the dissociation of the residual chains at the second treatment stage, the reactor of the gasification device comprises at least a second inlet for introducing the feed gases necessary for the gasification process at the second treatment stage, such as oxygen O₂ and water H₂O in the form of vapor.
In addition, the body of the gasification device may comprise a third inlet for the recovered gaseous fraction obtained as a result of the treatment of the feedstock material in suitable plants, when the device according to the invention is arranged downstream of said plants. For example, the recovered gaseous fraction may consist of carbon dioxide CO₂ in a proportion of 75% and the remaining part of 25% may consist of carbon monoxide CO, methane CH₄, and hydrogen H₂.
However, when the gasification device operates autonomously, feed gases useful for promoting the gasification process may be introduced into the third inlet.
The second dissociation means are preferably arranged lower than the inlets provided in the reactor for introducing the gases for the reaction of the second treatment stage.
The second dissociation means comprise second grids comprising at least one mobile grid and one fixed grid. Preferably, the fixed grid has a mesh size of about 3 mm for allowing passage of particles smaller than 3 mm. In addition, the fixed grid is surmounted by second heat storage means comprising a plurality of second spherical beads, preferably made of metal, for example iron, having a diameter between 70 mm and 90 mm, more preferably of 80 mm, for allowing passage of particles smaller than 3 mm. The mobile grid is adapted to move the second spherical beads in order to obtain dissociation of the particles of inert gases agglomerated at the second treatment stage and having a size larger than 3 mm.
Preferably, the purification system comprises a plurality of cyclones located close to the lower end of the reactor. The reactor is further provided with an outlet for the ashes coming from the purification operation performed by the cyclones, as well with a collector intended for collecting the ashes and preferably located at the lower end of the reactor.
In addition, the gasification device is provided with an outlet for the syngas obtained as a result of the gasification process carried out by the device.

Brief Description of the Drawings

A preferred embodiment of the invention will be described by way of non-limiting example with reference to the annexed Figures, in which:

Fig. 1 is a layout of a gasification device according to the invention;
Figs. 2-5 show corresponding details of the layout of Fig. 1;

Description of Some Preferred Embodiments of the Invention

Referring to Figs. 1-5, there is illustrated a preferred embodiment of a gasification device according to the invention, which has been indicated as a whole with reference numeral 10.
In the illustrated embodiment, the gasification device 10 comprises a body defined by at least one reactor 11, in which a first, upper end 11a and a second, lower end 11b are defined. The body 11 is provided with a corresponding inlet 13 for a certain amount of a carbonaceous feedstock material, said inlet being arranged at the first end 11a of the device 10, and at least one inlet 15 for introducing feed gases G1, G2 promoting performance of the gasification process. The feed gases G1, G2 are selected from carbon dioxide CO2, oxygen O₂ and water H₂O in the form of vapor.
The gasification device 10 is adapted to carry out at least two treatment stages, a first treatment stage S1 for the gasification of the solid fraction Fs of the feedstock material to be treated, by means of mixing with the feed gases G1, G2 introduced into the device 10, and a second treatment stage S2 for the dissociation of the gaseous fraction obtained at the first treatment stage.
In addition, a first dissociation of the complex gas molecules into simple molecules, obtained from the transformation of the solid fraction Fs into gaseous phase takes place at the first treatment stage S1.
In the illustrated embodiment, the temperature inside the reactor 11 at this first stage S1 is about 750°C.
The gasification device 10 comprises a check valve 17 for controlling the amount of solid fraction Fs entering the reactor 11. In the illustrated embodiment, the check valve 17 is a gate valve, more preferably a knife gate valve, made of steel and having adjustable frequency in order to vary the thickness of the solid fraction Fs.
Advantageously, the path of the solid fraction Fs inside the reactor 11 of the gasification device is from top to bottom, i.e. from the first, upper end 11a of the reactor towards the second, lower end 11b of the reactor, in order to define a path of the solid fraction Fs in co-current with the gaseous fraction obtained as a result of the gasification process, by exploiting the force of gravity.
In addition, in the illustrated embodiment, the reactor 11 is a cylindrical reactor with vertical axis and has a height of about 2 m and an outer diameter of about 1.5 m.
In the illustrated embodiment, the reactor 11 of the gasification device 10 is provided with two first inlets 15a, 15b for feed gases G1, G2 promoting the gasification process. The feed gases G1, G2 are selected from carbon dioxide CO₂, oxygen O₂ and water H₂O in the form of vapor.
In other embodiments, the reactor 11 may comprise more than two inlets, depending on the reactions to be obtained inside the reactor 11.
The gasification device 10 further comprises a gas distribution system 19 associated with the first inlets 15a, 15b for distributing the gases G1, G2 inside the reactor 11. In the illustrated embodiment, both the first inlets 15a, 15b and the gas distribution system 19 are arranged near the upper end 11a of the reactor 11 in order to guarantee the co-current path of the solid fraction Fs and the feed gases G1, G2.
The gas distribution system 19 comprises a housing 21 and at least one agitator 23 or mixer, movable, particularly rotatable, relative to the housing 21, and driven by a corresponding electric motor 25 and comprising mixing means 27 adapted to mix the gases G1, G2 coming from the first inlets 15a, 15b with the solid fraction Fs of the feedstock material entering the reactor 11. In the illustrated embodiment, the housing 21 has a cylindrical shape.
In the illustrated embodiment, the mixing means 27 comprise a plurality of first arms arranged in an axial direction on the body 29 of the agitator or mixer 23 and extending radially relative to the body 29 of the agitator or mixer 23.
In the illustrated embodiment, the first arms 27 extend radially over a plane substantially perpendicular to the longitudinal axis of the body 29 of the agitator 23 and are inclined downwards by an angle between 20° and 40° relative to said plane.
Advantageously, the first arms 27 of the agitator 23 are arranged in a sunburst pattern, offset relative to one another, in order to define a plurality of reaction layers R1, R2, R3, R4, said layers being associated with the inlets 15a, 15b of the reactor 11.
In the illustrated embodiment, the feed gases G1, G2 of the reactor 11 introduced through the inlets 15a, 15b comprise carbon dioxide CO₂, oxygen O₂ and water H₂O in the form of vapor, whose percentages vary depending on the temperature and the reaction to be obtained in each reaction layer R1, R2, R3, R4.
In the illustrated embodiment, in at least one of the reaction layers R1, R2, R3, R4 the reaction C + CO₂ = 2CO is promoted, allowing to increase the porosity of the residual carbon of the solid fraction Fs in order to obtain a catalyst for the dissociation of the complex gaseous molecules resulting from the mixing carried out by the agitator 23.
Other reactions obtained in the reaction layers may be 2C+O₂=2CO, 2H₂O+2CO=2H₂+2CO₂.
Advantageously, in the illustrated embodiment, each first arm 27 of the agitator 23 comprises a corresponding radial blade inclined by about 30° relative to a corresponding transverse plane, perpendicular to the body 29 of the agitator 23, for facilitating traveling of the solid fraction Fs downwards.
In addition, in the illustrated embodiment, both the body 29 and the first arms 27 of the movable agitator 23 are hollow, in order to allow the gases to flow into said body 29 and said arms 27.
The first arms 27 of the agitator 23 further comprise openings 31 for the exit of the gases. In the illustrated embodiment, the openings 31 are oriented downwards, i.e. towards the lower end 11b of the reactor 11. The openings 31 have a preferably circular shape and a diameter of about 3 mm. In addition, the openings 31 are arranged in one or more rows on respective first arms 27.
The gas distribution system 19 further comprises a plurality of second arms 33 stationary with respect to the housing 21 and arranged at three levels L1, L2, L3 in the illustrated embodiment. Each level L1, L2, L3 defined by the second stationary arms 33 is provided with a corresponding inlet nozzle 35 for the entry of the feed gases G1, G2 coming from the inlets 15a, 15b.
In the illustrated embodiment, each level L1, L2, L3 comprises two second stationary arms 33 associated with a single inlet nozzle 35 by means of an annular connector.
In addition, the second stationary arms 33 are arranged offset relative to the first arms 27 of the movable agitator 23.
The stationary arms 33 in turn comprise openings 31 for the exit of gases, said openings being oriented downwards and arranged in rows on said stationary arms 33. The openings 31 are preferably circular and have a diameter of about 3 mm.
The agitator 23 or mixer further comprises adjusting means for adjusting the speed of rotation to avoid areas of accumulation of the solid fraction Fs and obtain an optimal mixture as a result of the mixing of the solid fraction Fs with the feed gases G1, G2 of the reactor 11.
The gasification device 10 further comprises first dissociation means 39 for breaking the carbonaceous particles of the solid fraction Fs that have not been gasified yet. Considering that the reactor 11 is configured so as to guarantee a co-current path for the solid fraction Fs and the gaseous fraction obtained as a result of the dissociation of the solid fraction Fs at the first treatment stage S1, the first dissociation means 39 are arranged under the gas distribution system 19.
In the illustrated embodiment, the first dissociation means comprise first grids 29 comprising at least one mobile grid 41 moved by a corresponding motor 43 and at least one fixed grid 45.
The fixed grid 45 has a mesh size of about 5 mm and is surmounted by first heat storage means 47 up to a temperature of about 750°C, comprising a plurality of first iron spherical beads. In the illustrated embodiment, the spherical beads 47 have a diameter between 25 mm and 35 mm, more preferably a diameter of 30 mm, for allowing passage of particles smaller than 5 mm.
The mobile grid 41 is adapted to break the carbonaceous particles of the solid fraction Fs that have not been gasified yet. The mobile grid 41 is adapted to move the first spherical beads 47 at predetermined time intervals in order to obtain breakage of carbonaceous particles having a size larger than 5 mm.
In the illustrated embodiment, the first spherical beads 47 are arranged in layers on the fixed grid 45. Furthermore, the overall thickness of the layers of first spherical beads 47 is sized so as to obtain, as a result of the movement of the mobile grid 41, stirring and dissociation of the carbonaceous matter. In the illustrated embodiment, the first spherical beads 47 are arranged in two overlapping layers. Therefore, the overall thickness of the layers of first spherical beads 47 will be between 50 mm and 70 mm, preferably of 60 mm.
At the second treatment stage S2 of the gasification device 10, dissociation of the residual chains deriving from the first treatment stage S1 takes place in the presence of catalyst elements, such as for example the carbon particles exiting the first grids 39. In the illustrated embodiment, the reaction temperature at this second treatment stage S2 is about 850°C.
In order to carry out the dissociation of the residual chains at the second treatment stage S2, the reactor 11 of the gasification device 10 comprises at least a second inlet 49 for introducing gases G3 necessary for the reaction, such as oxygen O2 and water H₂O in the form of vapor.
In addition, the gasification device 10 comprises a respective third inlet 51 for the recovered gaseous fraction Fg obtained as a result of the treatment of the feedstock material in suitable plants, when the device 10 according to the invention is arranged downstream of such plants.
For example, the recovered gaseous fraction Fg may consist of carbon dioxide CO₂ in a proportion of 75% and the remaining part of 25% may consist of carbon monoxide CO, methane CH₄, and hydrogen H₂.
However, when the gasification device 10 operates autonomously, feed gases useful for promoting the gasification process may be introduced into the third inlet 51.
The gasification device 10 comprises second dissociation means 53 arranged lower than the inlets 49, 51 provided in the reactor 11 for introducing the gases G3, Fg for the reaction of the second treatment stage S2.
The second dissociation means comprise second grids 53 comprising at least one mobile grid 55, moved by a corresponding motor 57, and one fixed grid 59.
In the illustrated embodiment, the fixed grid 59 has a mesh size of about 3 mm for allowing passage of particles smaller than 3 mm. In addition, the fixed grid 59 is surmounted by second heat storage means 61 up to a temperature of about 850°C comprising a plurality of second iron spherical beads.
In the illustrated embodiment, the second spherical beads 61 have a diameter between 75 mm and 85 mm, preferably of 80 mm, for allowing passage of particles smaller than 3 mm. The second spherical beads 61, in the illustrated embodiment, are arranged in four layers on the fixed grid. The overall thickness of the layers of the second spherical beads 61 will be between 150 mm and 160 mm.
The mobile grid 55 moved by the motor 57 is adapted to move the second spherical beads 61 in order to obtain dissociation of the particles of inert gases agglomerated at the second treatment stage S2 and having a size larger than 3 mm.
The gasification device 10 further comprises a purification system 63 for the gases exiting the second treatment stage S2, for separating the gases from ashes. In the illustrated embodiment, the purification system 63 comprises a plurality of cyclones 63a, 63b, arranged near the lower end 11b of the reactor 11. The reactor 11 is further provided with an outlet 65 for the ashes coming from the purification operation performed by the cyclones 63a, 63b, as well with a collector 67 intended for collecting the ashes and located at the lower end 11b of the reactor 11.
The gasification device 10 further comprises an outlet 69 for the mixture of gases Gu obtained as a result of the treatment carried out at the second treatment stage S2. The mixture of gases Gu exiting the device 10 is a synthesis gas or "syngas". The synthesis gas may consist of carbon monoxide CO, carbon dioxide CO₂, hydrogen H₂ and water H₂O in the form of vapor.
The invention as described is susceptible to several modifications and variations falling within the same inventive principle.

Claims

A gasification device (10) for the valorization of substances contained in a carbonaceous feedstock material, said device comprising a reactor body (11) in which a first and a second end (11a, 11b) are defined, said reactor body being provided with a corresponding inlet (13) for said feedstock material (Fs) to be treated and with at least a first inlet (15) for introducing feed gases (G1, G2) into said body (11), wherein said device is configured to perform at least two treatment stages (S1, S2) for the gasification of said feedstock material (Fs) in order to obtain a syngas (Gu), characterized in that said device (10) further comprises:
- a gas distribution system (19) associated with said first inlet (15) in order to distribute the feed gases (G1, G2) inside the body (11) and comprising in turn mixing means (27) for mixing said gases (G1, G2) with said feedstock material (Fs) in order to obtain a first gasification of said feedstock material (Fs) at a first treatment stage (S1);

- first dissociation means (39) comprising first grids (39) and first heat storage means (47), and second dissociation means (53) comprising second grids (53) and second heat storage means (61) for performing a treatment of gasification of the molecules of the feedstock material (Fs) that have not been gasified at the first treatment stage (S1);

- a purification system (63) in which the gaseous fraction obtained from said treatment stages (S1, S2) is separated from the ashes derived from the gasification process;
and in that said gas distribution system (19), said first and second dissociation means (39, 53) and said purification system (63) are arranged in cascade from the first to the second end (11a, 11b) of the body (11) in order to promote a process of co-current gasification.
The device (10) according to claim 1, wherein said gas distribution system (19) comprises a housing (21) and at least one rotary agitator (23) driven by a corresponding motor (25) and movable relative to the housing (21), and wherein said mixing means comprise a plurality of first arms (27) associated with the body (29) of said agitator (23).
The device (10) according to claim 1 or 2, wherein said gas distribution system (19) comprises a housing (21) and said mixing means comprise a plurality of second arms (33) that are stationary relative to the housing (21) and arranged at levels (L1, L2, L3), each level being provided with a corresponding inlet (35) for said feed gases (G1, G2).
The device (10) according to claim 2 or 3, wherein said first arms (27) are arranged in a sunburst pattern, offset relative to one another on the body (29) of the agitator (23) in order to define a plurality of reaction layers (R1, R2, R3, R4), and wherein said body (29) of the agitator (23) and said arms (27) are hollow.
The device (10) according to claim 2, 3 or 4, wherein said first arms (27) extend radially over a plane substantially perpendicular to the longitudinal axis of the body (29) of the agitator (23) and are arranged inclined by an angle between 20° and 40° relative to said plane, in order to facilitate traveling of said feedstock material (Fs) downwards.
The device (10) according to claim 5, wherein said first arms (27) comprise radial blades inclined by about 30° relative to a corresponding transverse plane, perpendicular to the body (29) of the agitator (23), in order to facilitate traveling of the solid fraction (Fs) downwards.
The device (10) according to claim 3, 4 or 5, wherein said second arms (33) are arranged offset relative to said first arms (27), and wherein said first and second arms (27,33) comprise openings (31) for the exit of the gases.
The device (10) according to any of the preceding claims, wherein said first grids (39) comprise at least one mobile grid (41) and at least one fixed grid (45), and wherein said fixed grid (45) has a mesh size of about 5 mm and is surmounted by said heat storage means (47).
The device (10) according to claim 6, wherein said first heat storage means comprise metal spherical beads (47) arranged in layers on said fixed grid (45), and wherein said beads (47) have a diameter between 25 mm and 35 mm.
The device (10) according to any of the preceding claims, wherein said second grids (53) comprise at least one mobile grid (55) and at least one fixed grid (59), wherein said fixed grid (59) has a mesh size of about 3 mm and is surmounted by said heat storage means (61).
The device (10) according to claim 8, wherein said second heat storage means comprise metal beads (61) arranged in layers on said fixed grid (59), and wherein said beads (61) have a diameter between 70 mm and 90 mm.
The device (10) according to any of the preceding claims, wherein said purification system (63) comprises a plurality of cyclones (63a, 63b) arranged near the second end (11b) of the body (11), and wherein said body (11) is provided with an outlet (65) for the ashes deriving from the purification treatment as well as with an outlet (69) for the syngas obtained from the gasification of said feedstock material (Fs).