APPARATUS FOR COMBUSTION OF SYNTHETIC GASES DERIVING FROM TREATMENT OF ORGANIC MATERIAL, PLANT AND PROCESS FOR TREATMENT OF ORGANIC MATERIAL

Abstract

An apparatus for combustion of synthetic gases comprises a burner (75), a combustion chamber (62) cooperating with the burner (75) and having an outlet (64) destined to eject exhaust gases, a fluid supply circuit (65) configured for supplying a comburent gas to the burner (75), wherein the fluid supply circuit (65) is at least partially outside the combustion chamber (62) and has one or more channels (66) in contact with an outer surface (62a) of the combustion chamber (62) for exchanging heat with the combustion chamber itself. A plant and a process using the above combustion apparatus are also described.

Claims

1. Apparatus for combustion of synthetic gases deriving from the treatment of organic material, for example through pyrolysis, said apparatus comprising: a burner; a combustion chamber cooperating with the burner and having an outlet destined to eject exhaust gases; and a fluid supply circuit configured for supplying a comburent gas to the burner, wherein the fluid supply circuit is at least partially outside the combustion chamber and has one or more channels in contact with an outer surface of the combustion chamber for exchanging heat with the combustion chamber; wherein the burner comprises: a combustible access configured for receiving a combustible gas, a comburent access configured for receiving the comburent gas from the fluid supply circuit, a mixing chamber in communication with the comburent access and the combustible access for mixing said gases in inlet through said accesses, an activation device operating in the mixing chamber and configured for triggering the combustion of said gases.

2. Apparatus according to claim 1, wherein the fluid supply circuit has a gas access for receiving the comburent gas from an environment outside the combustion chamber and a gas outlet in communication with the combustion chamber or with the comburent access of the burner; and wherein the burner is placed upstream or internally to the combustion chamber.

3. Apparatus according to claim 1, wherein said one or more channels of the fluid supply circuit are formed from subsequent sections of a single continuous channel or from distinct channels in communication to each other, wherein said one or more channels are overlapped to a preponderant part of the outer surface of the combustion chamber.

4. Apparatus according to claim 1, wherein the combustion chamber extends along a development direction, and wherein said one or more channels of the fluid supply circuit are arranged transversely to the development direction of the combustion chamber.

5. Apparatus according to claim 1, wherein said one or more channels form at least a single continuous channel extending around the outer surface of the combustion chamber along a helical trajectory.

6. Apparatus according to claim 1, wherein said one or more channels form annular-shaped segments extending around to the outer surface of the combustion chamber, wherein each of said segments is in communication with an adjacent channel.

7. Apparatus according to claim 1, wherein the combustion chamber has a hollow tubular conformation; wherein the combustion chamber has a first and a second terminal wall which longitudinally delimit the combustion chamber; wherein the burner is carried by the first terminal wall; and wherein the fluid supply circuit contacts the outer surface from an area next to the second terminal wall until an area next to the first terminal wall.

8. Apparatus for combustion of synthetic gases deriving from the treatment of organic material, for example through pyrolysis, said apparatus comprising: a burner; a combustion chamber cooperating with the burner and having an outlet destined to eject exhaust gases; and a fluid supply circuit configured for supplying a comburent gas to the burner, wherein the fluid supply circuit is at least partially outside the combustion chamber and has one or more channels in contact with an outer surface of the combustion chamber for exchanging heat with the combustion chamber; wherein the fluid supply circuit comprises a sleeve which wraps the combustion chamber and is radially outside the outer surface of the combustion chamber to form a gap for receiving said comburent gas.

9. Apparatus according to claim 8, wherein the fluid supply circuit comprises one or more walls arranged transversely to a development direction of the combustion chamber, wherein subsequent sections of the one or more separating walls are parallel to each other; and wherein said one or more channels are laterally delimited by subsequent sections of the one or more separating walls and radially delimited by the sleeve.

10. Apparatus according to claim 9, wherein said walls extend radially, outside the outer surface of the combustion chamber and internally to the sleeve.

11. Apparatus according to claim 9, wherein said one or more walls are interconnected to each other to define a single helical element extending around the outer surface of the combustion chamber for a preponderant part or for all of a length of the combustion chamber measured parallel to the development direction.

12. Apparatus according to claim 8 comprising a case radially outside the sleeve which defines a gap between the sleeve and an inner surface of the case, wherein at least one of: the combustion chamber, the sleeve, and the case is devoid of coatings made in refractory or thermally insulating materials.

13. Apparatus according to claim 8, wherein the burner comprises an auxiliary access in communication with the combustion chamber for receiving combustible gas and allowing an initial ignition of the apparatus.

14. Apparatus according to claim 8, wherein the fluid supply circuit comprises a connection duct which connects the burner with a terminal part of the gap formed by said sleeve.

15. Apparatus for combustion of synthetic gases deriving from the treatment of organic material, for example through pyrolysis, said apparatus comprising: a burner; a combustion chamber cooperating with the burner and having an outlet destined to eject exhaust gases, wherein the combustion chamber extends along a development direction; a fluid supply circuit configured for supplying a comburent gas to the burner; wherein the fluid supply circuit is at least partially outside the combustion chamber and has one or more channels in contact with an outer surface of the combustion chamber for exchanging heat with the combustion chamber; wherein said one or more channels of the fluid supply circuit are formed from subsequent sections of a single continuous channel or from distinct channels in communication to each other; wherein said one or more channels overlap a preponderant part of the outer surface of the combustion chamber; and wherein said one or more channels of the fluid supply circuit are arranged transversely to the development direction of the combustion chamber.

16. Apparatus according to claim 15, wherein the fluid supply circuit has a gas access for receiving the comburent gas from an environment outside the combustion chamber and a gas outlet in communication with the combustion chamber or with the comburent access of the burner; and wherein the burner is placed upstream or internally to the combustion chamber.

17. Apparatus according to claim 15, wherein said one or more channels form a single continuous channel extending around the outer surface of the combustion chamber along a helical trajectory.

18. Apparatus according to claim 15, wherein said one or more channels form annular-shaped segments extending around to the outer surface of the combustion chamber, wherein each of said segments is in communication with an adjacent channel.

19. Apparatus according to claim 15, wherein the combustion chamber has a hollow tubular conformation; wherein the combustion chamber has a first and a second terminal wall which longitudinally delimit the combustion chamber; wherein the burner is carried by the first terminal wall.

20. Apparatus according to claim 19, wherein the fluid supply circuit contacts the outer surface from an area next to the second terminal wall until an area next to the first terminal wall.

Description

BRIEF DESCRIPTION OF THE DRAWING

[0325] Some embodiments and aspects of the invention will be described herein with reference to the accompanying figures, provided for illustrative purposes only and therefore not limiting wherein:

[0326] FIG. 1 is a perspective and schematic view of a plant for the treatment of organic material according to the aspects of the present invention;

[0327] FIG. 2 is a longitudinal cross-sectional view of a reactor according to the aspects of the present invention;

[0328] FIG. 3 is a detailed perspective view of a gas branch manifold of the reactor of FIG. 2;

[0329] FIG. 4 is a perspective view of the reactor of FIG. 2;

[0330] FIG. 5 is a further perspective view of a cross-section of the reactor of FIG. 2;

[0331] FIG. 6 a perspective view of a main conveyor that may operate in the reactor of FIG. 2;

[0332] FIGS. 7 and 8 are respective partially cross-sectional perspective views of a loading conveyor and an unloading conveyor usable with the reactor of FIG. 2;

[0333] FIG. 9 is a side section view of a burner according to the present invention;

[0334] FIG. 10A is a detail side view of a burner according to the present invention;

[0335] FIG. 10B is a longitudinal view of a burner variant according to other aspects of the present invention;

[0336] FIGS. 11 and 12 are respectively a perspective view and a side view of plant parts for the treatment of organic material according to the aspects of the present invention.

[0337] It is noted that in the present detailed description corresponding parts shown in the various figures are indicated with the same numerical references. Figures may illustrate the object of the invention through unscaled representations; therefore, parts and components shown in the figures relating to the object of the invention may relate exclusively to schematic representations.

[0338] Further, in the following description, reference is made to the accompanying figures of the drawing which form a part hereof, and in which are shown, by way of illustration, specific embodiments. It is to be understood that other embodiments may be utilized, and changes may be made without departing from the scope of the present invention.

DETAILED DESCRIPTION

Control Unit

[0339] At least one between the reactor and the plant herein described and claimed may comprise/use at least a control unit designed to control the operating conditions set up by the reactor itself and/or plant and/or to control the steps of the processes herein described and/or claimed.

[0340] The control unit may be a single unit or be formed by a plurality of distinct control units depending on design choices and operational requirements.

[0341] As a control unit it is intended a component of electronic type which may comprise at least one of: a digital processor (CPU), an analogue type circuit, or a combination of one or more digital processors with one or more analogue type circuits. The control unit may be configured or programmed to perform some steps: this may be practically made by any means that allows to configure or program the control unit. For example, in case of a control unit comprising one or more CPUs and one or more memories, one or more programs may be stored in appropriate memory banks connected to the CPU or CPUs; the program or programs contain instructions which, when executed by the CPU or by the CPU(s), program or configure the control unit to perform the operations described in relation to the control unit. Alternatively, if the control unit is/or comprises circuitry of an analogue type, then the circuit of the control unit may be designed to include circuitry configured, in use, to process electrical signals in such a way as to perform the steps related to the control unit. Parts of the process herein described may be made by means of a data processing unit or control unit, technically replaceable with one or more computers designed to carry out a portion of a software program or firmware uploaded onto a memory support. This software program may be written in any programming language of known type. The computers, if two or more in number, may be connected to each other by means of a data connection such that their computing powers are in any way shared; the same computers may thus be installed in geographically different locations as well, thereby realizing by means of the aforesaid data connection a distributed computing environment. The data processing unit, or control unit, may be a general-purpose processor configured to perform one or more parts of the process identified in the present invention via the software or firmware program, or being an ASIC or dedicated processor or an FPGA, specifically programmed to carry out at least part of the operations of the process herein described. The memory support may be non-transitory and may be inside or outside the processor, or control unit, or data processing unit, and can, specifically, be a memory geographically located remotely with respect to the computer. The memory support may also be physically divided into several portions, or in the form of cloud, and the software or firmware program may be stored on memory portions geographically divided to each other.

General Description of Plant 100

[0342] With reference to the accompanying figures, one illustrative embodiment of a plant for the thermochemical treatment of organic material, for example sludges from civil or industrial sewage, for producing a combustible gas subsequently referred to as synthetic gas, has been overall indicated with 100. Further carbonaceous residues, obtained by heating the organic material, may be refined to obtain further products such as, for example, active carbons.

[0343] As shown in FIG. 1, the plant 100 comprises a reactor 1 for the production of synthetic gas by means of heating the organic material at temperatures comprised between 400 C. and 800 C., in environments in the absence of oxidizing agents, at a controlled temperature and pressure. A heating of the reactor 1 at such temperatures implies a high energy consumption that may cause high operating costs of the plant. The present invention solves this drawback by using an apparatus 60 suitable for using the synthetic gas as combustible to generate heat useful for heating the reactor. In other words, the apparatus 60 allows, in cooperation with other elements of the plant 100 described below, to self-power the reactor 1 for treating the organic material and minimizing the operating costs of the plant itself. Additionally, the on-site combustion of the synthetic gas by means of the apparatus 60, avoids complex and expensive storage activities of the synthetic gas.

[0344] Before going into the details of the structure and operation of the individual elements that compose the plant 100, the general operation and structure of the plant will be described below, focusing on the interactions between the various components.

[0345] As mentioned, the reactor 1 comprises at least one heater active on a main channel 31 of the reactor 1 to heat, partially or integrally, a treatment chamber 2 inside the main channel 31, in which the organic material to be treated is located. The heater comprises a fluid heater 5 formed by a supply line 5a, for example helically shaped, whose coils are wound around the reactor, where circulates a heating fluid, optionally oil, for heating the organic material and transferring heat to the main channel 31. During the normal operation at steady state of the plant, the heating of the organic material results in the production of synthetic gas which is transferred, via a connection channel 81, to the apparatus 60 for being combusted when mixed with a comburent gas, optionally air. The supply of the comburent gas to the apparatus 60 may be made by means of a comburent gas supply line 85 for channeling the comburent gas itself, from an environment outside the plant, towards the apparatus 60. The plant 100 may also comprise a movement device 84, for example a fan, active on the comburent gas supply line 85 for supplying the comburent gas towards the apparatus 60. After the combustion of the synthetic gas with the comburent gas, an exhaust gas having a temperature comprised between 800 C. and 1000 C. is obtained, which is expelled from the apparatus 60 through an exhaust gases evacuation line 73 which channels it to a heat exchange unit 98 later described. The plant 100 may also comprise a suction device 120, for example a fan, operating on the exhaust gas evacuation line 73, to suck the exhaust gas from the apparatus 60, move it in the heat exchange unit 98 and expel it in the environment.

[0346] Unlike what has been described above which, as it has been said, refers to a condition of normal operation at steady state of the plant 100, in a condition of first start-up of the plant itself, and therefore in the absence of synthetic gas produced by the reactor, it is provided, by means of an auxiliary access 88, the forced supply of an exhaust gas, for example methane gas, for producing the exhaust gas useful for heating the heating fluid circulating in the reactor 1.

[0347] As mentioned above, the exhaust gas in the apparatus 60, is used by the heat exchange unit 98 for transferring heat to the heating fluid circulating in the fluid heater 5 of the reactor 1. The plant 100 may therefore have a recirculation line 108 that transfers the heating fluid of the fluid heater 5 from the reactor 1 until the heat exchange unit 98 is reached for being heated. In an example, the recirculation line 108 comprises a first branch 108a connected to a terminal end of the fluid heater 5 for channeling the heating fluid to the heat exchange unit 98, as well as a second branch 108b, connected to an initial end of the fluid heater 5, for receiving the heating fluid, opportunely heated, deriving from the heat exchange unit 98. The plant 100 may also comprise a recirculation pump 109, for example active on the first branch 108a of the recirculation line 108 as shown in FIG. 1, for moving the heating fluid through the branches of the recirculation line 108 itself and into the fluid supply line of the fluid heater 5. The plant may also comprise a recirculation valve 110 active on the recirculation line 108 for selectively allowing the passage on the second branch 108b of the recirculation line itself. In an example, the recirculation valve 110 may be a three-way diverter valve, having an inlet door 110a in communication with an upstream section of the second branch 108b, as well as a first and a second outlet door 110b, 110c, respectively in communication with the second and first branch 108b, 108a of the recirculation line 108. The plant may also comprise a connection branch 112 that connects the second outlet 110c of the recirculation valve 110 with the first branch 108a of the recirculation line 108. In a first operating condition, coinciding with a normal operating condition of the plant, the recirculation valve 110 allows exclusively the passage of the heating fluid along the second branch 108b of the recirculation line 108. Vice versa, in a second operating condition, the recirculation valve 110 exclusively allows the passage of the heating fluid along the connection branch 112 to reintroduce the heating fluid into the first branch 108a of the recirculation line 108, thereby isolating the reactor 1. The plant 100 may comprise a control unit 50 connected to the recirculation valve 110 and configured to control the movement thereof between the first and second operating condition if a cleaning procedure of the heat exchange unit 98 is performed, as described below. It is noted that the control unit commands the second operating condition of the recirculation valve 110 in order to facilitate the dissipation of heat retained by the heating fluid circulating through the heat exchange units, and to avoid vaporization, and therefore the ineffectiveness, of a cleaning fluid dispensed during the cleaning procedure. By reducing the temperature of the heating fluid, an efficient and effective cleaning of the heat exchange unit 98 may thus be realized.

[0348] The plant may further comprise a check valve 111 which operates in the first branch 108a of the recirculation line 108, in interposition between a joining point J between the connection branch 112 with the first branch 108a of the recirculation line and the reactor 1. This check valve 111 prevents, in the second operating condition of the recirculation valve 110, the passage of the heating fluid into the first branch 108a of the recirculation line, in the direction of the reactor 1.

[0349] As shown in detail in FIGS. 11 and 12, the plant 100 comprises a heat exchange unit 98 responsible for performing the heating of the working fluid by exploiting the exhaust gas in the apparatus 60. The heat exchange unit 98 may have a hot fluid chamber 98 destined to receive the exhaust gas deriving from the apparatus 60 and exchange heat with one or more cold fluid channels 98, present in the hot fluid chamber 98 and containing the heating fluid deriving from the fluid heater 5. In an example, the hot fluid chamber 98 has a hot fluid inlet connected to the exhaust gases evacuation line 73 and a hot fluid outlet 98b connected to the suction device 120. According to what is shown in FIGS. 11 and 12, the plant 100 may comprise a plurality of heat exchange units 98, interconnected to each other by means of upper 107a and lower 170b connection curves or joints, to define a single hot fluid chamber 98 that receives the exhaust gas from the exhaust gas evacuation line and channels it towards the suction device 120 for being expelled into the environment. Each cold fluid channel 98 may be a single duct or, if in presence of a plurality of heat exchange units, may have different sections interconnected to each other by connection ducts 122 housed in the upper and lower connection curves 107a, 107b, to define a single channel traversed by the heating fluid. It is noted that the cold fluid channel 98 is connected at its opposite ends to the first and to the second branch 108a, 108b of the recirculation line 108, defining, in cooperation with the recirculation line 108 itself and with the fluid supply line 5a of the fluid heater 5, a single closed-loop circuit.

[0350] The plant 100 may also comprise one or more collection containers 102, each of which located inferiorly and in communication with a respective heat exchange unit 98 for withdrawing dusts or solid debris which separate themselves from the exhaust gas in circulation in the hot fluid chamber 98. A loading cell 103 may be associated to each collection container 102 for generating a signal representative of a weight of the collection container itself: as a function of this signal it is possible to determine an alarm condition indicative of a maximum filling of the collection container 102. The control unit 50 connected to the loading cell/s 103 is configured for: [0351] receiving one or more signals generated by said loading cell/s 103, [0352] determining one or more measured values of weight of each collection container 102 as a function of the signals received from the respective loading cell 103, [0353] comparing each weight measured value of each collection container 102 with a threshold value of weight.

[0354] The control unit 50 is then configured for determining an alarm condition, as a function of the measured values of weight of each collection container 102, which commands an emitter 97 for reproducing an alarm signal (for example optical and/or acoustic) addressed to a user, in charge of performing a manual cleaning procedure of the collection container 102 and of one or more heat exchange units 98. Alternatively, the control unit 50 may be configured for commanding an automatic cleaning procedure of the heat exchange unit 98 which involves commanding the activation of one or more cleaning nozzles 106 inside the hot fluid chamber 98 of a respective heat exchange unit 98, for dispensing a cleaning fluid acting both in the hot fluid chamber 98 itself and in the collection tank 102. It is noted that the cleaning procedure additionally involves commanding the movement of the recirculation valve 110 from the first to the second operating condition.

[0355] The plant may also comprise one or more pressure sensors 104 which operate inside a hot fluid chamber 98 of a respective heat exchange unit 98, each of which configured for generating a pressure signal related to the pressure inside a respective hot fluid chamber 98. It is noted that the presence of pressure sensors 104 facilitates the determination of possible clogging in the hot fluid chambers 98 by means of the detection of the trend over time of the pressure in a predefined point of the heat exchange unit or pressure variation over the heat exchange unit itself.

[0356] The control unit 50 may be connected to each pressure sensor 104 and configured for: [0357] receiving one or more signals generated by each pressure sensor 104, [0358] determining one or more measured values of pressure as a function of the signals received from a respective pressure sensor 104, [0359] comparing said one or more measured values of pressure with a predefined criterion for assessing the presence or not of a clogging condition; for example each pressure measured value in a same point of the heat exchange unit 98 may be compared with a threshold pressure value for assessing whether or not there is a pressure drop which indicates the presence of clogging; alternatively pressure values between two points of the unit 98 may be compared for deducting the presence of pressure losses indicative of clogging.

[0360] Subsequently, the control unit 50 may be configured for determining an alarm condition if one or more measured values of pressure indicate the occurrence of clogging and subsequently, commanding the emitter 97 for the emission of an alarm signal or commanding the execution of the automatic cleaning procedure described above.

[0361] As for example shown in FIGS. 9, 10A and 11, the plant may also comprise a filter 91, optionally of cyclonic type, which operates on the exhaust gases evacuation line 73 upstream of the heat exchange unit 98, for separating dusts or debris mixed in the exhaust gas leaving the apparatus 60. The filter 91 may comprise an exhaust gases inlet 92, in communication with the exhaust gases evacuation line 73, for receiving the exhaust gas, as well as a filtered gas outlet 93 for channeling filtered gases in a downstream section of the exhaust gases evacuation line in direction of the heat exchange unit 98. The filter 91 may also comprise a debris outlet 94 in communication with a collection tank 95 for the deposit of solid particles separated from the exhaust gas. Associated to the collection tank 95, the filter 91 may have a loading sensor 96 for generating one or more signals representative of a weight of the collection tank itself and detecting a condition of maximum filling of the collection tank itself. The control unit 50 is connected to the loading sensor 96 and is configured for: [0362] receiving one or more signals generated by the loading sensor 96, [0363] determining one or more measured values of weight of the collection tank 95 as a function of the signals received from the loading sensor 96, [0364] comparing each weight measured value of the collection tank 95 with a threshold value of weight.

[0365] The control unit 50 is then configured for determining an alarm condition as a function of the measured values of weight of the collection tank 95, for example if these measured values of weight are greater than a threshold value of weight. This alarm condition involves commanding the emitter 97 for the reproduction of an alarm signal, for example optical or acoustic, or for commanding an automatic maintenance procedure of the filter.

[0366] The plant may also comprise a bypass line 99 connected to a section of the exhaust gases evacuation line 73 downstream of the outlet 64 of the apparatus 60, for deviating a flow of the exhaust gas directly in the environment without passing through the heat exchange unit 98 and/or the filter 91. It is noted that if the exhaust gas leaving the apparatus 60 has a temperature greater than a threshold value of temperature, optionally comprised between 800 C. and 1200 C., it is preferable to disperse directly into the environment the exhaust gas and avoid unwanted overheating and malfunctions of the heat exchange unit 98. For this purpose, the plant 100 may also comprise a bypass valve 101 which operates on the bypass line 99 for selectively allowing the passage of the exhaust gas through the bypass line itself. The plant 100 may also comprise an auxiliary gas movement device 123, for example a fan, active on the bypass line 99 for ejecting the exhaust gas into the atmosphere. The detection of the temperature of the exhaust gas is made by means of a temperature sensor 90, active on the outlet 64 of the apparatus 60 (FIG. 9) and configured for generating one or more signals representative of a temperature of the exhaust gas. The control unit 50 is connected to the temperature sensor 90 and is configured for: [0367] receiving one or more temperature signals generated by said temperature sensor 90, [0368] determining one or more measured values of temperature as a function of the signals received by the temperature sensor 90, [0369] comparing each measured values of temperature with the threshold value of temperature.

[0370] If the control unit 50 detects that one or more of the measured values of temperature, obtained by means of the temperature sensor 90, are greater than the threshold value of temperature, then the control unit 50 is configured for commanding an opening condition of the bypass valve for allowing the channeling of the exhaust gas in the bypass line 99 and, consequently, preventing the passage thereof towards the heat exchange unit 98.

[0371] To complete the description of the plant 100, the structure and the functionality of the single reactor 1 and the single apparatus 60 will be described in detail below.

Description of the Reactor 1

[0372] With reference to the accompanying figures which depict one illustrative embodiment of a reactor 1 for the treatment of organic material, suitable for preventing the formation and the transport of dusty particles mixed with synthetic gases produced by the reactor itself. As for example shown in FIG. 2, the reactor 1 comprises a main channel 31 which defines a treatment chamber 2 where it is performed a pyrolytic treatment of the organic material. The main channel 31 has an elongated body having tubular shape, optionally cylindrical, for example having constant cross section. The main channel 31 extends along a longitudinal development direction A between an inlet 3 for receiving organic material to be treated and an outlet 4, in communication with the inlet 3, destined to unload the treated organic material outside the treatment chamber 2. The inlet 3 is for example a radial opening defined at a terminal end of the elongated body of the main channel 31, whereas the outlet 4 is for example an axial opening of the main channel 31 opposite to the inlet 3.

[0373] The reactor 1 may also have a connection channel 30, cylindrical tubular-shaped, which puts in communication the outlet 4 of the main channel 31 with an unloading conveyor 16 subsequently detailed, for the unload of material treated in the main channel 31. As for example shown in FIG. 2, the connection channel 30 has an axial access 30a engaged to the outlet 4 of the main channel 31 and a radial outlet 30b opposite to the axial access 30a. The connection channel 30 is sloped with respect to the main channel 31, having the axial access 30a misaligned from the radial outlet 30b of the connection channel 30 with respect to a direction parallel to the longitudinal development direction A of the main channel 31. In other words, the radial outlet 30b of the connection channel 30 results located inferiorly to the axial access 30a and consequently inferiorly to the outlet 4 of the main channel 31.

[0374] The reactor 1 may also comprise a heater active on the main channel for heating the organic material present in the treatment chamber 2. In the following, reference is made in a non-limiting way, to a heater comprising a fluid heater 5 and an electric heater 6. However, it is possible to provide a single heater comprising exclusively a fluid heater or an electric heater or other types of heaters. As for example shown in FIGS. 2 and 5, the fluid heater 5 is active on a first section 2a of the main channel 31, next to the inlet 3 and extending for a preponderant part, optionally greater than the 60%, of an overall extension of the main channel measured between the inlet 3 and the outlet 4. The fluid heater 5 comprises a fluid supply line 5a which may be made with one or more ducts for the movement of a heating fluid. The ducts are placed in contact with an outer surface of the main body 31 for exchanging heat with an environment inside the main body 31 and heating the organic material. These ducts may have a single coil channel arranged along a helical trajectory around the main channel 31. In this regard, as shown in FIG. 5, the duct of the fluid supply line 5a of the fluid heater 5, may be formed by a helical sheet arranged radially around the main channel 31 of the reactor and upperly delimited by a tubular case 63 radially outside the main channel 31. The channel of the fluid supply line 5a where the heating fluid flows is then laterally delimited by successive sections of the helical sheet, whereas it is radially delimited by the outer surface of the main channel 31 and by the tubular case 63.

[0375] As previously mentioned (see FIG. 1), the fluid heater 5 may be connected to the first and to the second branch 108a, 108b of the recirculation line 108 for supplying, by means of the first branch 108a of the recirculation line 108, the heating fluid, optionally at low temperatures, to the heat exchanger and receiving, by means of the second branch 108b of the recirculation line itself, the heating fluid, at high temperatures. The connection between the fluid supply line 5a of the fluid heater 5 and the recirculation line may be made by means of connectors positioned at opposite ends of the fluid supply line 5a itself, allowing the inlet of hot heating fluid at an area of the line 5a next to the inlet 3 of the main channel 31 and supplying, from the side opposite to the inlet 3, cold fluid to the recirculation circuit 108. A fluid-tight connection between the fluid supply line 5a and the heat exchange unit 98, optionally made by connectors, allows the movement of relatively hot fluid in the reactor 1 and the discharge of relatively cold fluid from the reactor. The cooled fluid, after being reheated as previously detailed, is recirculated back to the reactor 1.

[0376] As previously mentioned, the heater may also comprise an electric heater 6 active on a second section 2b of the main channel 31 interposed between the first section 2a and the outlet 4 of the main channel 31. The second section 2b extends for a terminal section of the main channel 31 next to the outlet 4, having a length lower than the first section 2a. The organic material may be almost totally heated by the fluid heater 5, whereas it may be only marginally heated by the electric heater 6. The electric heater 6 may comprise one or more electrical resistances in contact with the outer surface of the main channel 31 for heating the organic material when connected to the power grid.

[0377] The reactor 1 may also comprise a temperature sensor 28, active in the treatment chamber 2 in proximity of a gas outlet opening 8 and connected to the control unit 50 which is responsible for controlling the temperature of the fluid heater 5 and the electric heater 6. The temperature sensor 28 is configured for generating one or more signals representative of a temperature inside the treatment chamber 2, used by the control unit 50 for determining one or more measured values of temperature to be compared with a threshold value of temperature comprised between 280 C. and 800 C., optionally comprised between 320 C. and 680 C. The control unit 50 may also be connected to both the fluid heater 5 and to the electric heater 6 for commanding the functioning thereof as a function of measured values of temperature. Optionally the control unit 50 may command the heaters 5 and 6 in a completely independent manner, implementing dedicated control strategies for each heater. A temperature control strategy may for example involve heating the treatment chamber 2 by means of the fluid heater 5, until a first threshold is reached, for example comprised between 250 C. and 450 C., followed by heating by means of the electric heater 6 until a second temperature threshold is reached, optionally comprised between 400 C. and 800 C. It is noted however that both control logics implementable by the control unit 50, use as temperature feedback signal the signals provided by the temperature sensor 28.

[0378] The reactor may also comprise a pressure sensor 29 active in the treatment chamber 2 and configured for allowing the control unit 50 to maintain a substantially constant level of pressure in the treatment chamber 2: the pressure in the treatment chamber is for example constantly maintained lower than the environmental pressure present in the environment outside the reactor. The control unit 50 is connected to the pressure sensor 29 and is configured for: [0379] receiving one or more pressure signals generated by said pressure sensor 29, [0380] determining one or more measured values of pressure as a function of the signals received from the pressure sensor 29, [0381] verifying if said one or more of the measured values of pressure indicate that the pressure inside the treatment chamber is lower than the environmental pressure, reigning outside the plant.

[0382] According to an aspect the control unit 50 verifies if one or more of the measured values of pressure indicate that the pressure inside the treatment chamber is lower than the environmental pressure by a quantity comprised in a reference range between 10 Pa and 250 Pa, optionally between 20 Pa and 100 Pa.

[0383] If one or more measured values of the relative pressure in the reactor 1 are external to the above specified reference range, the control unit 50 is configured for commanding the suction device 120 for adjusting consequently the ejection of the synthetic gas from the main channel 31.

[0384] As for example shown in FIG. 7, the reactor 1 may comprise a loading conveyor 15 which operates in proximity of the inlet 3 of the main channel 31 for moving organic material in the treatment chamber 2. The loading conveyor 15 may be a screw or auger conveyor which operates inside a loading channel 12a engaged, at a first end 15a, to the inlet 3 of the main channel 31 for defining, in cooperation with the latter, a single channel. The loading channel 12a is laterally engaged to the main channel 31 at or in immediate proximity of the inlet 3 of the main channel 31, where, by means of an axial access, communicates with the treatment chamber 2. The loading channel 12a may also have, at a second end 15b opposite to the first end, an inlet mouth 32a configured for receiving organic material from a hopper 33 subsequently described. In an example, the inlet mouth 32a may have a connection shank radially emerging from the loading channel 12a for facilitating the connection with the hopper 33. The loading channel 12a and consequently the loading conveyor 15 are sloped with respect to the main channel 31, with the second end 15b which is located inferiorly to the first end 15a. In other words, the loading channel 12a is sloped with respect to a horizontal plane by an inner angle comprised between 10 and 85, optionally comprised between 20 and 70. It is noted that this inclination of the loading channel 12a determines, during the steps of loading, the movement against gravity of the organic material, preventing the lifting and the supply of dusts in the treatment chamber 2 of the main channel 31. The reactor 1 may also comprise a motor 14a connected to the loading conveyor 15 at the second end 15b, for moving the loading conveyor 15 with respect to the loading channel 12a. The reactor 1 may also comprise said control unit 50, connected to the motor 14a associated to the loading conveyor 15, configured for commanding the movement thereof as a function of a predetermined speed profile, optionally at constant speed.

[0385] As previously mentioned, the reactor 1 may also comprise or be associated to a hopper 33 connected to the loading conveyor 15 and configured for storing the organic material to be treated in the treatment chamber 2. The hopper 33 may have a container having a truncated pyramid shape or an inverted cone shape, equipped with an unloading opening 34 on a lower end of the container, for discharging the organic material downstream in the direction of the loading conveyor 15. The hopper 33 may also comprise an unloading channel 35 which connects the unloading opening 34 of the hopper with the inlet mouth 32a of the loading channel 12a, defining a single fluid tight connection which prevents the dispersion of dusts in the environment. The reactor 1 may also comprise a conveyor or an auger, activated by an electric motor, active on the unloading channel 35 for controlling the movement of organic material towards the loading channel 12a.

[0386] As for example shown in FIG. 6, the reactor 1 comprises a main conveyor 17 which operates in the main channel 31, for moving the organic material under treatment in the treatment chamber 2, from the inlet 3 to the outlet 4 along a predetermined treatment path inside the main channel 31. The main conveyor 17 may be a screw or auger conveyor having a shaft 18 movable by rotation about an axis parallel to the longitudinal development direction A of the main channel 31, from which radially emerge one or more helical rotors 19 interconnected to each other to define a coil. At least one of said helical rotors 19 is a solid rotor 24 extending seamlessly until in proximity of an inner surface of the main channel 31, for moving the material under treatment towards the outlet 4. In other words, each solid rotor 24 has an outer surface devoid of cavities for maximizing the area of contact with the material under treatment and efficiently moving it towards the outlet 4. The main conveyor 17 has a respective solid rotor 24 with one or more coils, at ends of the shaft 18 respectively next to the inlet 3 and to the outlet 4 of the main channel 31 and having hollow rotors 20 or wings 25 described below, at an intermediate section between the inlet and the outlet 3, 4 of the main channel 31.

[0387] In an example, one or more helical rotors 19 are hollow rotors 20, i.e. have a cavity 22 defining a passage radially interposed between the shaft 18 of the main conveyor 17 and a perimeter edge 21 of the hollow rotor 20 which surrounds the shaft 18. It is noted that the cavity 22 of each hollow rotor 20 allows not only the passage of organic material under treatment, but also the passage of synthetic gases generated by heating of the organic material itself, thereby increasing the efficiency of the treatment. The presence of hollow rotors 20 prevents also a movement of synthetic gases through the material under treatment, thus avoiding the lifting of dusty particles which, when mixed with the synthetic gas, contribute to reduce the overall quality of the synthetic gas.

[0388] The hollow rotors 20 may be engaged to the shaft 18 by means of an adjacent solid rotor 24 or by means of one or more transversal spokes 23 which connect respective sections of the perimeter edge 21 to the shaft 18. In an example, each hollow rotor may have one or more spokes 23 angularly offset to each other by an angle comprised between 70 and 110, even more optionally comprised between 80 and 100, for conferring structural rigidity to the hollow rotors 20. The main conveyor 17 may also comprise one or more wings 25 radially emerging from the shaft 18 until at the inner surface of the main channel, configured for moving the material under treatment in contact with the inner surface itself of the main channel 31. The wings 25 allow to mix the organic material under treatment and, bringing it into contact with the inner surface of the channel, make the heat transmission with the main channel 31 more efficient. Referring again to FIG. 6, the main conveyor 17 comprises a plurality of wings 25 angularly offset to each other, for example by an angle comprised between 70 and 200, optionally comprised between 80 and 100. Each wing may have a curved terminal body 25b which contacts the inner surface of the main channel 31, connected to the shaft 18 of the main conveyor 17 by a rod 25a. The terminal body 25b of each wing may be a platelike body lying on a plane transversal to a horizontal plane passing by the shaft 18 and transversal to the rod 25a, conferring to the wing a substantially T or L profile. As previously mentioned, the helical rotors 19 with one or more coils and the wings 25, cover a central section of the shaft 18 for moving the material under treatment from the inlet 3 towards the outlet 4 of the main channel 31. The main conveyor 17 may be divided in sectors adjacent to each other and having helical rotors 19 or wings 25. In detail, the main conveyor may comprise at least a first and a second sector having respectively helical rotors 19 with one or more coils and a plurality of wings 25, alternated to each other for a preponderant part of the length of the shaft 18, optionally covering at least 70% of the length of the shaft itself. For moving the material under treatment in the treatment chamber 2, the main conveyor 17 may have respective first sectors with solid rotors 24, in proximity of the inlet 3 and of the outlet 4 of the main channel 31. The reactor 1 may also comprise a motor 26 connected to the main conveyor 17 for allowing a movement thereof with respect to the treatment chamber 2 when activated by the control unit 50. The control unit 50 may be connected to the motor and configured for commanding the movement of the main conveyor 17 at a constant angular velocity or as a function of a predetermined speed profile.

[0389] The ejection of the treated organic material in the treatment chamber 2 is made by an unloading conveyor 16 which operates in proximity of the outlet 4 of the main channel 31 (FIG. 8). Similarly to the loading conveyor 15, also the unloading conveyor 16 may be a screw or auger conveyor which operates inside an unloading channel 12b connected to the radial outlet 31a of the connection channel 31a for defining, in collaboration with the radial outlet 31a, a single channel suitable for preventing the dispersion of dusts in the environment. The unloading channel 12b is laterally engaged to the connection channel 31a at a first end 16a in communication with the treatment chamber 2. The unloading channel 12b may also have, at a second end 16b opposite to the first end 16a, an outlet mouth 32b configured for unloading the treated organic material withdrawn from the treatment chamber 2 towards a deposit station not shown in the accompanying figures. The unloading channel 12b and consequently the unloading conveyor 16 are sloped with respect to the main channel 31, where the second end 16b of the unloading conveyor 16 is located above the first end 16a of the unloading conveyor 16 itself. In other words, the unloading channel 12b is sloped with respect to a horizontal plane, by an inner angle comprised between 10 and 85, optionally comprised between 20 and 70. It is noted that the inclination of the unloading channel 12b determines the movement against gravity of the treated organic material, preventing the lifting of dusts in the treatment chamber 2 of the main channel 31. The reactor 1 may also comprise a motor 14b connected to the unloading conveyor 16 at the second end 16b, for moving the unloading conveyor 16 with respect to the unloading channel 12b. The control unit 50 may be connected to the motor 14b associated to the unloading conveyor 16 and configured for commanding the movement thereof as a function of a predetermined speed profile, optionally at constant speed.

[0390] As shown in FIGS. 3 and 4, the reactor 1 comprises also a gas outlet opening 8 defined on the main channel 31 for expelling from the main channel 31 the synthetic gases produced during the treatment. The gas outlet opening 8 is located at an upper half of the main channel 31 next to the outlet 4, at a minimum distance Dm from the outlet 4 of the main channel 31 greater than the vertical dimension D1 of the main channel 31. In other words, the gas outlet opening 8 is positioned at a terminal section of the main channel 31 next to the outlet 4, having extension equal to no more than of the main channel. From the dimensional point of view, the ratio between the minimum distance Dm and the overall length L of the main channel 31, measured parallel to the longitudinal development direction A of the main conveyor 17, is comprised between 0.1 and 0.3. It is noted that the particular position of the gas outlet opening 8 in a terminal area of the reactor next to the outlet 4 of the main channel 31, allows the ejection of synthetic gases heated by the electric heater 6 having temperature next to 600 C. The gas outlet opening 8 has an elongated shape parallel to the longitudinal development direction A of the main channel 31, having a length lower than the length L of the main channel 31. In other words, the ratio between the length of the gas outlet opening 8 and the length L of the main channel 31 measured parallel to the longitudinal development direction A of the main conveyor 17 is comprised between 0.1 and 0.5.

[0391] The reactor 1 comprises a gas branch manifold 7 suitable for supplying the synthetic gases generated in the main channel towards the burner 60. The specific structure of the gas branch manifold 7 and, subordinately, the positioning thereof with respect to the main channel 31, allow to convey the synthetic gases mixed with reduced quantities or total absence of dust particles. With reference to FIGS. 2 and 3, the gas branch manifold 7 comprises a proximal portion 7a connected to the main channel 31 at the gas outlet opening 8 and a distal portion 7b, spaced from the gas outlet opening, having a gas discharge orifice 10 for channeling the synthetic gas towards the burner 60. It is noted that providing a gas discharge orifice 10 spaced from a gas outlet opening 8 on the main channel 31, limits the lifting against gravity of dusts which tend to precipitate in the main channel 31. In this way it is possible to channel, towards the burner 60 and by means of the connection channel 81, synthetic gases comprising a limited quantity of dusts which could cause clogging and malfunctioning of the burner such that the normal functioning thereof may be impaired. In an embodiment shown in FIG. 2, the gas branch manifold 7 may have a prismatic or cylindrical tubular conformation, having a constant passage area for all the extension thereof from the proximal portion 7a to the distal one 7b. The gas branch manifold 7 may also comprise an expansion section 7c extending along a direction radially exiting the main channel 31, in interposition between the proximal portion 7a and the distal portion 7b. By means of the expansion section 7c is possible to further limit the lifting of dusts mixed with synthetic gases which lose speed once they reach the expansion section 7c, resulting in the precipitation of dusts towards the main channel 31 and allowing only the synthetic gases to exit the reactor 1 via the gas discharge orifice 10. As for example shown in FIG. 2, the expansion section 7c extends radially, optionally vertically, from the gas outlet opening 8, positioning the distal portion 7b of the gas branch manifold 7 at a maximum height H from the gas outlet opening 8. From a dimensional point of view, the maximum height H of the gas branch manifold 7 and the vertical dimension D1 of the main channel 31 is comprised between 1.2 and 2.5. The gas discharge orifice 10, located in the distal portion 7b, is in an area of the gas branch manifold 7 at maximum distance from the gas outlet opening 8. Additionally, the gas discharge orifice 10 has a gas passage area lower than a gas passage area of the gas outlet opening 8 from the main channel. By reducing the cross section of the gas discharge orifice 10 it is possible to increase the ejection speed of the synthetic gases, casing the withdrawal of the gases to be conveyed to the combustion apparatus 60 described in detail below.

Description of the Combustion Apparatus 60

[0392] Moving on now to describe one illustrative embodiment of the apparatus 60 for the combustion of synthetic gases, it comprises, as previously mentioned, a combustion chamber 62 for the combustion of synthetic gases, for example generated in the reactor 1. The combustion chamber 62 receives, by means of the connection channel 81, synthetic gases passing through the gas discharge orifice 10 of the reactor 1, as well as it has an outlet 64 destined to eject exhaust gases in the exhaust gases evacuation line 73.

[0393] As for example shown in FIGS. 9, 10A and 10B, the combustion chamber 62 has a hollow tubular conformation extending along a development direction X. In the accompanying figures it has been shown a cylindrical combustion chamber 62, however, it is not excluded the realization of a combustion chamber having a prismatic conformation with a polygonal section, for example square or rectangular. The combustion chamber 62 has an inner volume perimetrically delimited by an inner surface, optionally cylindrical, and longitudinally delimited by a first and a second terminal wall 62, 62 of the combustion chamber 62. The combustion chamber 62 also has an outer surface 62a optionally having a cylindrical conformation, in contact with fluid supply circuit 65 described in the following.

[0394] The apparatus also comprises a burner 75 for example carried by the first terminal wall 62 or working inside the combustion chamber and responsible for realizing the combustion of the synthetic gases in the combustion chamber 62. In an example, the burner 75 may comprise a combustible access 77 in communication with the connection channel 81 for receiving the synthetic gas from the reactor 1, as well as a comburent access 76 suitable for receiving the comburent gas from the fluid supply circuit 65. The burner 75 may also comprise a mixing chamber 78 where the synthetic gases and the comburent gas are mixed and an activation device 72, for example an electric or spark plug ignition, triggers the combustion of the synthetic gas and with the comburent gas (alternatively the mixing of the two gases may take place directly in the combustion chamber without a different mixing chamber).

[0395] The burner 75 may also comprise an auxiliary access 88 in communication with the mixing chamber 78 for receiving a combustible gas and allowing an initial ignition of the apparatus as previously detailed.

[0396] As mentioned, the apparatus comprises a fluid supply circuit 65 destined to supply a comburent gas, optionally ambient air, to the burner and/or to the combustion chamber 62. The fluid supply circuit 65 (for example a preponderant part thereof) contacts the outer surface 62a of the combustion chamber 62, from an area close to the second terminal wall 62 where it has a gas access 67 for receiving the comburent gas from an outer environment, until an area next to the first terminal wall 62 where it has a gas outlet 68 in communication with the comburent access 76 of the burner 75. The fluid supply circuit 65 may comprise one or more channels 66 placed outside and in contact with the outer surface 62a of the combustion chamber 62 for channeling the comburent gas, optionally air, towards the combustion chamber 62 itself. It is noted that the temperature of the comburent gas entered in the combustion chamber 62, contributes to increase the efficiency of the combustion process of the synthetic gases and furthermore, avoids the generation of undesired condensation and/or the formation of solid particles or dusts in the combustion chamber 62 which may compromise the normal operativity thereof. The positioning of the channels 66 in contact with the outer surface 62a of the combustion chamber 62 allows the heat exchange with the channels 66 of the fluid supply circuit 65, causing the heating of the comburent gas. Additionally, the channels 66 in contact with the outer surface 62a of the combustion chamber 62, define a thermally insulating layer which avoids the need of realizing the combustion chamber 62 itself in ceramic materials or covering the chamber with insulating or refractory materials for allowing the combustion of the synthetic gas at temperatures comprised between 800 C. and 1000 C. As further consequence there is the possibility of making the combustion chamber 62 having a more essential structure, for example realizable exclusively in metallic materials, optionally stainless steel, thus leading to a reduction of the costs of realization of the entire apparatus.

[0397] It is also noted that the channels 66 of the fluid supply circuit 65 may contact a preponderant part, optionally at least the 70%, of the outer surface 62a of the combustion chamber 62 for increasing the heat exchange surface with the combustion chamber itself. For this purpose, the channels 66 may be arranged transversely to the development direction X of the combustion chamber 62 and formed by successive sections of a single continuous channel extending along a helical trajectory (see FIG. 10A), or by different annular-shape channels, in fluid communication to each other (FIG. 10B). Referring again to FIGS. 9, 10A and 10B, the fluid supply circuit 65 may comprise a sleeve 68 which wraps the combustion chamber 62 outside the outer surface 62a of the combustion chamber 62 itself, to form a gap destined to receive the comburent gas and radially delimiting the channels 66. The fluid supply circuit 65 may also comprise one or more walls 69 emerging from the outer surface 62a of the combustion chamber 62 until in proximity of the sleeve 68, for laterally delimiting the channels 66. Furthermore, the walls develop longitudinally for a preponderant part of a, optionally for all the, length of the combustion chamber 62 measured parallel to the development direction X, following a helical trajectory or following respective annular trajectories. According to what has been previously described, the walls 69 may form optionally equidistant successive sections along the development direction X, forming part of a single helical body (FIG. 10A) or may form respective annular bodies which delimit respective segments 66a of a channel 66 (FIG. 10B). Preferentially, the comburent gas entered in the fluid supply circuit 65, may be circulated within a single channel 66 laterally delimited by successive sections of a wall 69 itself and radially delimited by the outer surface 62a of the combustion chamber 62 and by the sleeve 68.

[0398] The fluid supply circuit 65 may also comprise a connection duct 74 which connects a terminal section of the supply circuit 65 next to the first terminal wall 62, with the burner 75 or with the combustion chamber, for supplying the comburent gas in inlet to the combustion chamber 62.

[0399] The apparatus may also comprise a case 70 radially outside the sleeve 68 which defines a further gap between the sleeve 68 and an inner surface 70a of the case itself 70. This gap defined by the case 70 may optionally delimit an air bag having insulating or dissipating functions for the heat emitted by the combustion chamber 62.

[0400] Concerning materials, the sleeve 68, the walls 69 and the case 70 are made in metallic material, optionally stainless steel, devoid of coatings made of refractory or thermally insulating materials.

Process for the Treatment of Organic Material

[0401] One or more embodiments of the present invention include a process for the treatment of organic material by means of the plant 100 according to the above description and according to the accompanying aspects and/or the accompanying claims.

[0402] In one or more embodiments, the process involves a thermochemical treatment of the organic material, optionally in granular or dust form, made by means of the reactor 1, for obtaining a combustible gas, subsequently indicated as synthetic gas, exploited by the apparatus 60 for generating heat and self-heating the reactor itself. The process initially involves supplying organic material in the treatment chamber 2 of the reactor 1, for example performing a step of unloading the organic material on the loading conveyor 15, followed by a step of moving the organic material itself towards the inlet of the treatment chamber 2 of the reactor 1. The process may comprise a step of controlling the speed of movement of the loading conveyor 15 for avoiding the lifting of dusts which could lead to malfunction to the reactor 1.

[0403] It is then expected a following step of moving, by means of the main conveyor 17, the organic material from the inlet 3 to the outlet 4 of the main channel 31. Simultaneously to moving the material, the process may also comprise a step of heating, performed by means of the fluid heater 5 and the electric heater 6, at a temperature comprised between 250 C. and 800 C., optionally comprised between 280 C. and 600 C.

[0404] The process also comprises a step of withdrawing the treated organic material from the treatment chamber 2 for being stored. For example, the step of withdrawing involves moving, by means of the unloading conveyor 16, the organic material outside the treatment chamber 2 of the reactor 1, controlling the movement speed of the unloading conveyor 16 itself, for preventing or limiting the lifting of dusts which could mix with the synthetic gas. The process may then comprise a step of withdrawing, by means of the gas branch manifold 7, the synthetic gas obtained by heating the treatment chamber 2. The step of withdrawing may in turn involve sucking the synthetic gas at a speed comprised between 0.05 m/s and 0.8 m/s, optionally comprised between 0.1 m/s and 0.4 m/s and/or a step of adjusting a pressure in the treatment chamber 2 such that this pressure is lower than the pressure of the environment outside the plant, for example such that the absolute inner pressure (assuming to use the plant described herein and claimed on the sea level) is comprised between 101320 Pa and 101000 Pa, optionally comprised between 101305 Pa and 101200 Pa. More generally, the pressure inside the treatment chamber 2 is maintained from 5 to 325 Pa, optionally 20 to 125 Pa, below the environmental pressure.

[0405] A step of transporting, by means of the connection channel 81, synthetic gas, from the reactor 1 towards the burner 75 of the apparatus 60 may follow the withdrawal of the synthetic gas from the reactor 1. The process may then comprise a step of channeling, by means of the comburent gas supply line 85, a comburent gas, optionally air, in the fluid supply circuit 65 of the apparatus 60, which, once heated, will be supplied to the combustion chamber 62 and therefore to the burner 75. The progressive advancement of the comburent gas in the fluid supply circuit 65 towards the burner/combustion chamber, involves a gradual heating of the comburent gas itself until a temperature greater than 250 C., optionally comprised between 450 C. and 650 C., is reached before being entered in the combustion chamber or supplied to the burner 75. In an example, the process involves channeling the comburent gas according to a helical or annular trajectory along the fluid supply circuit 65, so as to maximize the heat exchange between the combustion chamber 62 and the comburent gas. After supplying of the synthetic gas and of the comburent gas in the mixing chamber 78 of the burner 75 or directly in the combustion chamber, the process may involves triggering the combustion between these gases by means of the activation device 72.

[0406] The process may then comprise a step of withdrawing an exhaust gas in the combustion chamber 62 of the apparatus 60 and channeling it in the exhaust gases evacuation line 73 in direction of the heat exchange unit 98 or channeling it in the bypass line 99 if having at a temperature greater than the threshold value of temperature, optionally comprised between 900 C. and 1200 C. In order to perform heating of the fluid destined to the fluid heater 5 of the reactor 1, the process may involve conveying, in the hot fluid chamber 98 of the heat exchange unit 98, the exhaust gas leaving the apparatus 60. The process may simultaneously involve supplying the fluid to be heated destined to the fluid heater 5, in one or more cold fluid channels 98 of the heat exchange unit 98. The heat exchange between hot fluid chamber 98 and each cold fluid channel 98, involves heating the heating fluid which, by means of the second branch 108b of the recirculation line 108, is again entered in the fluid supply line of the fluid heater 5 of the reactor 1. The exhaust gas, after having exchanged heat with the heating fluid of the fluid heater 5 of the reactor 1, is ejected into an environment outside of the plant.

[0407] The process may also comprise for a step of discharging dusts present in a collection container 102 associated to a respective heat exchange unit 98, performed on the basis of the detection of the weight of the collection container itself by means of the loading cell 103. The process may then comprise a cleaning procedure of each heat exchange unit 98 for removing any clogging of dusts or debris such as to compromise the normal functioning of the heat exchange unit itself. In an example, the cleaning procedure may involve the activation of cleaning nozzles 106 for the emission of water jets in the hot fluid chamber 98 of the heat exchange unit 98 and in the collection container 102.

[0408] The process may also comprise a step of filtering the exhaust gas leaving the apparatus 60 and upstream of the heat exchange unit 98, for withdrawing dusts or solid debris mixed in the exhaust gas, which will be then deposited in the collection tank 95. If clogging of the filter 91 is detected, the process may comprise a maintenance procedure which involves discharging dusts from the collection tank 95 if one or more weight values of the collection tank 95 itself are greater than a threshold value of weight.

[0409] Any references and publications cited herein are expressly incorporated herein by reference in their entirety into this disclosure, except to the extent they may directly contradict this disclosure. Although specific illustrative embodiments have been described herein, it will be appreciated by those of ordinary skill in the art that a variety of alternate and/or equivalent implementations can be substituted for the specific embodiments shown and described without departing from the scope of the present disclosure. It should be understood that this disclosure is not intended to be unduly limited by the illustrative embodiments and examples set forth herein and that such examples and embodiments are presented by way of example only with the scope of the disclosure intended to be limited only by the claims.