ITMI20130320A1 - CONVERSION PLANT OF CARBONOUS MATRICES, PARTICULARLY FOR THE PRODUCTION OF ENERGY, AND ITS PROCEDURE. - Google Patents

Description

"CARBON MATRIX CONVERSION PLANT, PARTICULARLY FOR THE PRODUCTION OF ENERGY, AND RELATED PROCEDURE"

DESCRIPTION

The present invention relates to a plant for converting carbonaceous matrices, particularly for the production of energy, and the related process for converting carbonaceous matrices.

Gasification plants are currently known which make it possible to dispose of material containing Carbon and Hydrogen, while at the same time producing energy, for example in the form of synthesis gas.

These materials, hereinafter also referred to as "carbonaceous matrices", can be: biomass, vegetable fats or flours, organic fractions of agricultural, urban, industrial and hospital waste, civil and industrial water purification sludge, tires and rubbers, polymeric materials or elastomeric or thermoplastic or duroplastic, tar sands or sands containing hydrocarbons, asphalt and tars, tar coatings, contaminated soils, composite materials, electrical and electronic waste.

Gasification is a process of thermal degradation that occurs at high temperatures in the presence of a sub-stoichiometric percentage of an oxidizing agent, such as air, oxygen or steam and allows, on the one hand, to solve the ecological problem connected to the elimination of the aforementioned waste and waste materials, and on the other hand to obtain energy, as well as synthesis gas. Synthesis gas, also known as "syngas" in jargon, is in fact a synthetic fuel gas that can be suitably treated and then cleaned, to then be used for the production of electricity, for example by combustion in engines or gas turbines.

Known carbon matrix conversion plants, used for energy production, are not free from drawbacks, including poor energy production efficiency.

In particular, if such known plants produce synthesis gas, this synthesis gas generally has a low calorific value.

A further criticism of known plants concerns the inefficiency of heat exchange between the heating parts of the plant and the carbonaceous matrices to be heated for their conversion into synthesis gas.

Another criticism of these known types of plants concerns the effects of wear, friction and corrosion of the transport members of the carbonaceous matrices, and the risk of jamming of the transport members themselves, with consequences both on the performance of the plant and on its maintenance. .

A further criticism of these known types of plants concerns the risk of ignition of explosion or fire of parts of the plant, related to possible uncontrolled exothermic reactions due to the presence of abnormal concentrations of oxygen and / or air in some part of the plant. , or to the aforementioned jams, which can produce localized overheating.

Another drawback of such known plants consists in the fact that the carbonaceous matrix is often not energetically and homogeneously mixed and crushed during the conversion phase into synthesis gas, and this reduces the conversion efficiency.

A further drawback of these known types of plants consists in the lack of the catalytic effect performed by the thermally conductive bodies during the phase of conversion of the carbonaceous matrix into synthesis gas.

Furthermore, in known plants, the synthesis gas production efficiency is strongly constrained by the type of carbonaceous matrix introduced into the plant. In fact, these plants are not sufficiently flexible in receiving a wide variety of materials to be converted in input.

A further drawback of known types of plants relates to the inefficient conversion and abatement of the waste by-products obtained from the conversion of carbonaceous matrices into synthesis gas, which, accumulating, lead to the obstruction of the passage ducts of the plant, requiring continuous maintenance.

The main aim of the present invention is to provide a conversion plant for carbonaceous matrices, particularly for the production of energy, which solves the technical problems described above, obviates the drawbacks and overcomes the limits of the prior art, allowing to considerably increase efficiency. conversion of carbon matrices and energy production.

Within this aim, an object of the invention is to allow an efficient production of synthesis gas, both in terms of volume of gas produced and in terms of its caloric power characteristics.

A further object of the present invention is to provide a plant where the heat exchanges between the heating parts and the carbonaceous matrices to be heated are particularly efficient.

Another object of the invention is to provide a plant which does not require maintenance due to wear, friction, corrosion and jamming of the moving parts.

A further object of the invention is to provide a plant which is capable of giving the greatest guarantees of reliability and safety in use, preventing the triggering of explosions and / or fires.

Another object of the invention is to provide a plant which allows to produce synthesis gas free of critical compounds, such as nitrogen oxide, ammonia or other viscous and insoluble by-products such as tars.

Another object of the invention is to provide a plant which is economically competitive if compared to the known art.

The aforementioned task, as well as the aforementioned purposes and others which will appear better later, are achieved by a carbon matrix conversion plant, particularly for the production of energy, comprising a carbon matrix conversion station, which comprises:

- a reaction chamber where a synthesis gas is extracted from a carbonaceous matrix,

- a combustion chamber adapted to generate a heating thermal vector, for heating said reaction chamber, e

- an expansion tower, where said synthesis gas is separated from solid products,

and comprising a filtering and cooling station for said synthesis gas leaving said expansion tower,

characterized in that said reaction chamber comprises an internal tubular element able to rotate with respect to a longitudinal rotation axis, and an external tubular element concentric to said internal tubular element, said internal tubular element comprising, on the external lateral surface, a plurality of blades defining, along at least a longitudinal portion of said external lateral surface of said internal tubular element, a plurality of channels for the advancement, along said reaction chamber, of said carbonaceous matrix and of said synthesis gas forming from said carbonaceous matrix , said heating thermal vector flowing inside said internal tubular element.

Furthermore, the aforementioned task, as well as the aforementioned purposes, are achieved by a process for the conversion of carbonaceous matrices, comprising the steps of:

- extracting synthesis gas from a carbonaceous matrix, in a reaction chamber;

- generating a heating thermal vector, for heating said reaction chamber,

- separating said synthesis gas from solid products in an expansion tower,

- filtering and cooling said synthesis gas leaving said expansion tower,

characterized in that said step of extracting synthesis gas from said carbonaceous matrix comprises the steps of:

- starting from said reaction chamber comprising an internal tubular element able to rotate with respect to a longitudinal rotation axis, and an external tubular element concentric to said internal tubular element, said internal tubular element comprising, on the external lateral surface, a plurality of blades, defining, along at least a longitudinal portion of said external lateral surface of said internal tubular element, a plurality of channels, to advance said carbonaceous matrix and said synthesis gas being formed by said carbonaceous matrix along said channels;

- making said heating thermal vector slide inside said internal tubular element.

Further characteristics and advantages will become clearer from the description of a preferred but not exclusive embodiment of a carbonaceous matrix conversion plant, particularly for the production of energy, illustrated by way of non-limiting example with the aid of the attached drawings in which:

Figure 1 is a schematic representation of an embodiment of a carbonaceous matrix conversion plant, particularly for the production of energy, according to the invention; Figure 2 is a partial longitudinal sectional view of the carbon matrix conversion station of the plant of Figure 1, according to the invention;

Figure 3 is a longitudinal section view of the elements inside the reaction chamber of the station for converting carbonaceous matrices of Figure 2, according to the invention;

Figure 4 is a sectional view of the elements inside the reaction chamber represented in Figure 3 taken along the axis IV IV;

Figure 5 is a sectional view of the elements inside the reaction chamber represented in Figure 3 taken along the V - V axis;

Figure 6 is a partially cut-away perspective view of the elements inside the reaction chamber shown in Figure 3;

Figure 7 is a perspective view of the reaction chamber shown in Figure 2;

Figures 8 and 9 are respectively a cross-sectional view and a front elevation view of a first embodiment of an expansion tower of the carbon matrix conversion station of Figure 2;

Figures 10 and 11 are respectively a cross-sectional view and a front elevation view of a second embodiment of an expansion tower of the carbon matrix conversion station of Figure 2;

Figures 12 and 13 are respectively a cross-sectional view and a front elevation view of a third embodiment of an expansion tower of the carbon matrix conversion station of Figure 2;

Figure 14 is a schematic representation of the bypass system of the plant in Figure 1.

With reference to the aforementioned figures, the plant for converting carbonaceous matrices, particularly for the production of energy, generally indicated with the reference number 1, comprises a station for converting carbonaceous matrices 2 into a synthesis gas 20 and a station for filtration and cooling 7, 8, 9 of the synthesis gas 20 leaving the conversion station 2.

In particular, the synthesis gas conversion station 2 20 comprises:

- a reaction chamber 3 where the synthesis gas 20 is extracted from the carbonaceous matrix inserted in correspondence with an inlet 22 of the reaction chamber 3 itself,

a combustion chamber 4 adapted to generate a heating thermal vector 40, for heating the reaction chamber 3, e

- an expansion tower 5, where the synthesis gas 20 is separated from the solid products 21 originating from the carbonaceous matrix.

According to the invention, the reaction chamber 3 comprises an internal tubular element 30 able to rotate with respect to a longitudinal rotation axis 31, and an external tubular element 300 concentric to the internal tubular element 30. The internal tubular element 30 comprises, on the its external lateral surface 32, a plurality of blades 33, 34 defining, along at least a longitudinal portion of the external lateral surface 32 of the internal tubular element 30, a plurality of channels 35 for the advancement, along the reaction chamber 3, of the carbonaceous matrix and of the synthesis gas 20 forming from the carbonaceous matrix. The heating thermal vector 40, generated by the combustion chamber 4, flows inside the internal tubular element 30.

Then, the thermal vector 40 generated by the combustion chamber 4 passes inside the internal tubular element 30, while in the annular section space comprised between the external tubular element 300 and the internal tubular element 30 it advances along the aforementioned channels 35 defined by the blades 33, 34 the carbonaceous matrix which, during the advancement, due to the heating effect, is converted into synthesis gas 20.

Advantageously, moreover, the direction of advancement, along the reaction chamber 3, of the carbonaceous matrix and of the synthesis gas 20 forming from the carbonaceous matrix, is opposite to the longitudinal flow direction of the thermal vector 40 inside the internal tubular element. 30.

The thermal vector 40 is advantageously constituted by inert hot air.

The carbonaceous matrix is introduced into the reaction chamber 3 at the inlet 22 and is made to advance along the reaction chamber 3 towards the expansion tower 5. During this advancement, the carbonaceous matrix is exposed to a gradually increasing temperature due to the the fact that the thermal vector 40 flows inside the internal tubular element 30, composed of the high temperature fumes leaving the combustion chamber 4. Along this path, therefore, the carbonaceous matrix absorbs the heat transmitted by the thermal vector 40, exchanging it through the internal tubular element 30 and the blades 33, 34, advantageously made of thermally conductive material and capable of withstanding high temperatures, and convert into synthesis gas 20.

The material in which the internal tubular element 30, the external tubular element 300 and the blades 33, 34 are advantageously of the type known under the trademark ICONEL 601 ®, capable of withstanding temperatures even in the order 1200 ° C.

In steady-state operation of the plant 1, and in particular of the reaction chamber 3, at the outlet from the reaction chamber the carbonaceous matrix is completely converted into synthesis gas 20 and solid products 21.

Furthermore, advantageously, the channels 35 defined by the blades 33, 34 are wound in a spiral around the internal tubular element 30, and the rotation of the internal tubular element 30 and of the blades 33, 34 determines the advancement along the reaction chamber. 3, due to the cochlea effect, of the carbonaceous matrix and of the synthesis gas 20. The aforementioned spiral winding of the channels 35 is illustrated, by way of example, with a dash-dot line 36 in figure 6.

In correspondence with the inlet 22 to the reaction chamber 3 there is advantageously provided an auger 23 which serves to introduce and advance the carbonaceous matrix in the initial part of the reaction chamber 3. In the remaining part of the reaction chamber 3, the advancement of the carbonaceous matrix, during the conversion to synthesis gas 20, occurs due to the rotation of the internal tubular element 30 which holds the poles 33, 34, which, for the their spiral arrangement around the internal tubular element 30, precisely define the aforesaid channels 35, which produce the cochlea effect. During the advancement, the carbonaceous matrix continues to absorb the heat coming from the heating vector 40, thanks to the heat exchange guaranteed by the blades 33, 34 and in particular by the contact surface they make available.

Alternatively, or in addition to the aforementioned auger effect, the rotation axis 31 of the internal tubular element 30 can be advantageously inclined with respect to a horizontal direction, so that the rotation of the internal tubular element 30 and of the blades 33, 34 determines , due to gravity, the advancement of the carbonaceous matrix along the reaction chamber 3.

Advantageously, moreover, the external tubular element 300 is able to rotate together with the internal tubular element 30 and the blades 33, 34. In other words, the external tubular element 300, the internal tubular element 30 and the blades 33, 34 between the two tubular elements, they rotate as a single body, and have no parts in relative movement with respect to each other.

The internal tubular elements 30 and external 300 are advantageously supported rotatably by two fixed heads 301, 302, placed at the ends of the tubular elements themselves.

Figures 6 and 7 illustrate the reaction chamber 3. Figure 6 illustrates the external tubular element 300, which comprises an external shell 307 and an internal refractory 309, suitable for reducing heat exchange with the external environment. The external tubular element 300 is made integral with the blades 33, 34 by means of brackets 308. These brackets 308 are engaged on one side in the external tubular element 300, and on the other hand they are associated with the blades 33 which, given their folded configuration, illustrated in the section of Figure 4, are elastically pressed against the brackets 308 and thus ensure the transmission of the rotation motion between the internal tubular element 30 and the external tubular element 300. Figure 7 illustrates the support rollers 310 of the external tubular element 300, which engage with circumferential rolling bands 311.

In the reaction chamber 3 thus described, the heat exchange between the heating vector 40 and the carbonaceous matrices does not occur only through the external lateral surface 32 of the internal tubular element 30, but rather through the large exchange surface defined by the blades 33, 34. In addition to this, the appropriate thermal insulation of the external tubular element 300, by means of the refractory 309, allows to reduce to a minimum the thermal dispersions towards the outside, favoring the achievement of the temperatures necessary for the conversion of the matrices carbonaceous in synthesis gas 20.

Advantageously, moreover, as illustrated in Figure 4, each of the blades 33 is folded and has an L-shaped conformation, with a radial end folded inwards, so as to increase the contact surface with the carbonaceous matrix. Furthermore, this L-shaped conformation causes the succession of the radial blades 33 to define, as illustrated in particular in Figure 6, well-defined channels 35, for the advancement of the carbonaceous matrix and of the synthesis gas 20 being formed.

In the reaction chamber 3, in fact, two chambers with opposing flows are created: in the first chamber, where the carbonaceous matrix to be treated is inserted, thanks to the auger effect, the advancement of the carbonaceous matrix is allowed, which therefore passes through all the reaction phases, up to the discharge of the process solid products; in the second chamber, consisting of the internal part of the internal tubular element 30, the thermal vector 40 flows in countercurrent with respect to the advancement of the carbonaceous matrix.

This thermal vector 40, before releasing its heat to the carbonaceous matrix, has temperatures ranging between 1100 ° C and 1200 ° C, while in the phase of leaving the reaction chamber 3 it has lower temperatures, depending on the heat exchange that has taken place. in the reaction chamber 3 itself.

The contact of the carbonaceous matrix introduced into the reaction chamber 3, with the internal tubular element 30 and the blades 33, 34 triggers the so-called pyrolysis phenomenon, which consists in the thermochemical decomposition of organic and non-organic materials, obtained by applying heat in the complete absence of an oxidizing agent (usually oxygen). The reactions which take place in the reaction chamber 3 are in fact exothermic reactions which take place in the absence of oxygen.

The carbonaceous matrix exchanges heat with the thermal vector 40 without ever coming into contact with it. In fact, it slides outside the internal tubular element 30, in the channels 35 defined by the blades 33, 34, gradually increasing its temperature, counter-current with respect to the flow of the thermal vector 40, until, in steady state, complete or partial gasification. depending on the process requirements. In fact, at the end of its path along the reaction chamber 3, the carbonaceous matrix can be completely absent because it is transformed into solid (residual) and gaseous (synthesis gas 20) components, in the case of complete gasification. In the case of partial gasification of the carbonaceous matrix, it will be transformed into synthesis gas 20 and solid by-products of various types.

Advantageously, the internal tubular element 30, in a portion near the expansion tower 5, or in a portion located at least partially inside the expansion tower 5, has blades 34 arranged radially so as to define a finned pack, such as the one illustrated in figure 5. This finned pack is advantageously made with radial blades 34 in sheet metal, inclined by about 3 ° with respect to a longitudinal direction, so as to be able to also act as an auger and allow solid residues (or by-products) originating from the transformation of the carbonaceous matrix into gas 20 meaning that it can be discharged and fall to the bottom of the expansion tower 5 itself, where means for recovering the powders 25 are advantageously arranged, consisting for example of an auger with relative storage tank.

Furthermore, since these radial blades 34 of the finned pack are located right next to the combustion chamber 4, they have a temperature advantageously around 1100 ° C, capable of further raising the temperature of the synthesis gas 20 passing through the finned pack. , bringing it from about 700-750 ° C to about 900 ° C, temperature at which the gasification of the carbonaceous matrix can be complete, to the point of being able to gasify any tars or TARs (by-products of pyrogasification processes including organic compounds and / or aromatic rings).

The solid residues are expelled from the finned pack defined by the radial blades 34, in the bottom of the expansion tower 5, while the synthesis gas 20 produced rises upwards in the expansion tower 5, favored by the fact that the environment of the tower expansion tube 5, in direct communication with the environment of the reaction chamber 3, is advantageously kept in constant depression, ensuring an upward flow of gas having a speed not exceeding 0.5 meters per second. This low speed of the flow guarantees the further decantation on the bottom of the expansion tower 5 of coarse particulate matter or dust present in the synthesis gas 20.

The expansion tower 5 advantageously also comprises means for the injection of air or oxygen 50, 51, 52 for raising the temperature of the synthesis gas 20 which passes through it.

In fact, in the event that the synthesis gas 20, after passing through the finned pack, does not reach the desired complete gasification temperature, of about 900 ° C, the air or oxygen injection means 50, 51, 52 are activated. in substoichiometric ratio.

This operation, under temperature control, allows a sub-stoichiometric micro-combustion of the tars and TARs still present in the synthesis gas 20, which allows the design temperatures to be reached.

This phase, also called "gas reforming phase", is used in particular in the case in which structural changes occur in the carbonaceous matrix introduced into the reaction chamber 3, where the introduction of a carbonaceous matrix richer in powders, or with a reduced calorific value determines a <1> inertization of the gasification phase, with a lowering of the temperature of the reaction chamber 3 itself. In this case, the working temperatures of 900 ° C are not reached at the outlet from the finned pack, but will be reached in the expansion tower 5 due to the air and / or oxygen injection means 50, 51, 52.

The air and / or oxygen injection means 50, 51, 52 advantageously comprise distribution manifolds 53, positioned perimeter to the expansion tower 5, and connected to injection nozzles 54 of the air and / or oxygen inside the itself.

The number of injection nozzles 54 is advantageously proportional to the quantity of air and / or oxygen to be introduced into the expansion tower 5. The injection nozzles 54 are advantageously positioned so as to create an air and / or oxygen knife which extends transversely substantially over the entire cross section of the expansion tower 5.

The air and / or oxygen injection means 50 comprise, according to a first embodiment illustrated in Figures 8 and 9, cylinders 501 of pure oxygen connected by means of a modulating valve 502 to the manifolds 53. The modulating valve 502 is operated by a controller 503, which receives information relating to the temperature values inside the expansion tower 5 from a temperature sensor 504, such as a thermocouple.

According to a second embodiment illustrated in Figures 10 and 11, the air and / or oxygen injection means 51 comprise a compressor 511 connected through a modulating valve 502 to the manifolds 53. The modulating valve 502 is operated by a controller 503, which receives information relating to the temperature values inside the expansion tower 5 from a temperature sensor 504, such as a thermocouple.

According to a third embodiment illustrated in Figures 12 and 13, the air and / or oxygen injection means 52 comprise a fan 521. To adjust the flow rate of the fan 521, which through the controller 503 connected to the temperature sensor 504 Ã It is able to decrease or increase the number of revolutions of the fan 521 and consequently the flow of injected air, keeping the temperature of the synthesis gas 20 constant.

The carbonaceous matrix conversion plant 1 also advantageously comprises a by-pass station 6 suitable for collecting the synthesis gas 20 leaving the expansion tower 5 and burning it in the atmosphere during the start-up phase of the plant 1.

In fact, during the start-up phase of the plant 1, as there are not yet all the ideal conditions for the production of synthesis gas 20, a three-way valve 60 is provided at the outlet of the expansion tower 5 which allows the station to be bypassed of filtration and cooling 7, 8, 9 of the synthesis gas, thus avoiding an unnecessary clogging of the filtration systems.

By means of a high temperature fan 61, the synthesis gas 20 is sucked in and sent to a torch 62 and burned in the atmosphere.

The fan 61 advantageously puts also the internal environments of the reaction chamber 3 and of the expansion tower 5 under constant depression. Advantageously, the flow of gas passing through the pipes 64 of the by-pass station 6 has a speed in the order of 20 meters per second, a speed that prevents the particulate from being able to attach itself to the walls of the pipes. Moreover, advantageously, the pipes 64 are perfectly thermally insulated to prevent the tars present in the synthesis gas 20 from condensing and depositing on the walls of the pipes, clogging them. The temperature of the synthesis gas 20 in this phase is however kept above about 350 ° C, since the dew point of the tars and TARs starts at about 300 ° C. The fan 61 is put in communication with an atmospheric air intake 65, for cooling it, through a first on-off valve 66. The flow of gas from the fan 61 towards the torch 62 can be interrupted by a second valve on-off 67. Before escaping into the flare 62, the gas passes through a hydraulic seal 68.

The filtration and cooling station 7, 8, 9 of the synthesis gas 20 comprises:

a station with cooled cyclones 7, - a station with bag filters 8,

- a heat exchange station 9.

In particular, the filtration and cooling station 7, 8, 9 includes:

- at least one cyclone 70, 71 adapted to abate the particulate matter present in the synthesis gas 20;

- at least one bag filter 80 adapted to purify the synthesis gas 20 from micro-particles present in the synthesis gas 20;

- at least one heat exchange battery 90, 91 suitable for lowering the temperature of the synthesis gas 20.

The synthesis gas 20, in passing through the aforesaid stations, is also advantageously subject to respective temperature drops.

According to the embodiment of the plant 1 illustrated in Figure 1, the synthesis gas 20, exiting the expansion tower 5 by now purified of the tars produced by pyrolysis, advantageously enters a first cyclone 70 and subsequently into a second cyclone 71, where it deposits part of the particulate not removed by the expansion tower 5. In particular, the gas entering the cyclones 70, 71 is forced into a spiral motion in the interspace between two cylinders that define the cyclone, from top to bottom. Particles with greater inertia tend to hit the walls of the outermost cylinder and fall to the bottom of the cyclone, where they are recovered. Furthermore, the spiral motion allows the gas to come into contact with the cold wall of the cyclone cylinder and consequently release calories and lower its own temperature. The cold wall of the cyclone is generally water-cooled by means of 72 cooling fans.

The synthesis gas 20, which has a temperature of about 900 ° C, enters the first cyclone 70 leaving it at a temperature of about 500 ° C, and enters the second cyclone 71 at about 500 ° C, leaving it at a temperature of about 250 ° C.

Subsequently, the synthesis gas 20 enters a special high temperature bag filter 80, where the gas is perfectly purified from the micro-particulate, collected in an accumulation tank 82. The bags of the bag filter 80 are cyclically washed in counter-current with nitrogen from a nitrogen production plant 81.

The synthesis gas 20 leaves the bag filter 80 at a temperature of about 230-240 ° C and enters a first gas / air exchanger 90, which uses atmospheric air to cool the tube bundle and consequently the gas. The gas temperature is then lowered to around 90 ° C.

The gas then passes through a second gas / water exchanger 91, connected to a refrigeration unit 93, which brings the temperature of the synthesis gas to about 5 ° C. At this temperature the water vapor present in the synthesis gas 20 generated by the humidity of the gasified carbonaceous matrix is condensed making the gas totally dehydrated. The condensate is collected in a tank 94.

The fact of providing a first gas / air exchanger 90, upstream of the second gas / water exchanger 91, allows to reduce the power required for the refrigeration unit 93, and consequently also the electricity consumption.

A high-pressure fan 102 puts all the aforementioned machinery in constant depression. All regulation systems are managed by a controller connected to thermocouples, pressure switches and flow regulators.

A synthesis gas 20 can contain up to 70 different types of tars, each type of tar has its own physical-chemical characteristics, among which, in particular, the "dew point", that is the temperature and pressure conditions at which the tar contained in a condensate gas. The fact of providing multiple temperature drops of the synthesis gas 20 passing through the various stations 7, 8, 9 of the filtration and cooling station, favors the gradual elimination of the various types of tar, thus reducing, in each station 7, 8 , 9 clogging due to the possible deposition of condensed tar.

At the outlet of the filtration and cooling station 7, 8, 9, part of the synthesis gas 20 thus produced can be conveyed to the combustion chamber 4 through the pipe 104, to be burned and produce the thermal vector 40 for heating the chamber reaction 3.

The remaining part of the syntesis gas thus produced can instead be used to generate electrical and / or thermal energy, for example by means of a motor generator 103, or possibly burned in a torch 105.

The process for converting carbonaceous matrices, which can be advantageously carried out through the plant for converting carbonaceous matrices, according to the invention, comprises the steps of:

- extracting synthesis gas 20 from a carbonaceous matrix, in a reaction chamber (3);

- generating a thermal vector 40 for heating the reaction chamber 3;

- separating the synthesis gas 20 from the solid products 21 in an expansion tower 5;

- filtering and cooling the synthesis gas 20 leaving the expansion tower 5.

According to the invention, the step of extracting synthesis gas 20 from a carbonaceous matrix comprises the steps of:

- starting from a reaction chamber 3 comprising an internal tubular element 30 able to rotate with respect to a longitudinal rotation axis 31, and an external tubular element 300 concentric to the internal tubular element 30, where the internal tubular element 30 comprises, on the external lateral surface 32, a plurality of radial blades 33, 34, defining, along at least a longitudinal portion of the external lateral surface 32 of the internal tubular element 30, a plurality of channels 35, to advance the carbonaceous matrix and the synthesis gas 20 in formation from the carbonaceous matrix along the channels to cause the heating thermal vector 40 to flow inside the internal tubular element 30.

The filtering and cooling station 7, 8, 9, according to the present invention, is not necessarily linked to the station for converting carbonaceous matrices 2 according to the present invention. In fact, this filtration and cooling station 7, 8, 9 can be applied to any plant for the production of a synthesis gas at high temperatures, for example around 900 ° C, solving the technical problem of filtering and cooling the gas itself, up to temperatures in the order of 5 ° C, in order to prevent the deposition of condensed tar and thus avoid the clogging of cyclones, filters, pipes and exchangers that make up the filtration and cooling station itself. In fact, the filtration and cooling station 7, 8, 9, according to the present invention, allows to control and manage the sequence of temperature drops of the gas to be filtered and cooled so as to optimize its cleaning.

In practice it has been found that the plant for converting carbonaceous matrices, particularly for the production of energy, according to the present invention, fulfills the intended aim and objects as it allows to convert carbonaceous matrices into energy, in an efficient manner. .

Another advantage of the invention consists in the fact that it allows the production of synthesis gas with a high caloric power.

Another advantage of the plant, according to the invention, consists in maximizing the efficiency of the heat exchanges between the heating parts and the carbonaceous matrix to be heated. In particular, this is achieved because the carbonaceous matrix advances in a space, between the two tubular elements, outside the space where the thermal vector flows, and because an extensive and controllable exchange surface is provided in the reaction chamber. thermal, defined by the external surface of the internal tubular element and the blades that branch off from it. To this is added the effect due to the counter-current sliding of the thermal vector with respect to the advancement of the carbonaceous matrix along the reaction chamber.

The result is such that the plant according to the invention is capable of generating a gaseous stream, and therefore a synthesis gas with a calorific value up to three times higher than that of known plants, and as such , with the same generation of electrical and thermal energy, it produces a third of the weight of synthesis gas and solid residues, and therefore also a third of fumes. Consequently, with the same energy generation, the dimensions and costs of the plant according to the invention are lower than conventional plants.

A further advantage of the plant, according to the invention, consists in the fact that it requires minimal maintenance interventions to solve problems due to wear, friction, corrosion and jamming of the moving parts. In fact, the fact that the tubular elements and the blades are integral and rotate together prevents non-homogeneous thermal expansions from causing ovalization of the tubular elements and consequent eccentric rotations capable of causing excessive wear.

Furthermore, since the external tubular element is not mobile relative to the blades, the risks of jamming of material between moving parts relative to each other are excluded, thus preventing localized overheating which can also lead to the ignition of explosions and / or fires, making the plant according to the invention extremely reliable and safe in use.

In addition to this, the constant depression of the internal environments of the reaction chamber and of the expansion tower prevents the formation of uncontrolled gas pockets which could give rise to explosions and / or fires.

A further advantage of the plant, according to the invention, consists in allowing the production of synthesis gas free of critical compounds, such as nitrogen oxide, ammonia or other viscous and insoluble by-products such as tars. In fact, unlike known plants, where gasification takes place in a few minutes and the retention time of the combustible gaseous stream is very short, in the plant according to the invention the carbonaceous matrix that enters the reaction chamber remains there even for times higher than an hour, being exposed to gradually higher temperatures until reaching 900 ° C and therefore a complete gasification, in which even the tar can be substantially gasified.

During the start-up phase of the plant, not being able to guarantee a complete gasification of the carbonaceous matrix, a by-pass station is provided, to avoid unnecessary blockages of the pipes and of the cooling and filtration systems of the gas.

In addition to this, where, for various reasons, including changes in the calorific value of the inlet carbonaceous matrix, it is not possible to guarantee a temperature of 900 ° C in the reaction chamber, this temperature is in any case reached, by means of the of gas and / or air injection, in the expansion tower.

A further advantage of the plant, according to the invention, consists in ensuring good mixing and good crushing of the carbonaceous matrix inside the reaction chamber, thanks to the slow and constant rotation of the radial blades, which prevents the matrix carbonaceous layer to lie down, due to gravity, on the bottom of the reaction chamber, but it forces it to advance, continuously and homogeneously, along the passage channels defined by the radial blades themselves.

Furthermore, thanks to the extended contact surface between the radial blades heated by the thermal vector and the carbonaceous matrix, through the use of metals or special additives, it is possible to increase the catalytic effect performed by the thermally conductive bodies.

Another advantage of the plant, according to the invention, consists in the fact that it can be flexibly adapted to the conversion, into synthesis gas, of carbonaceous matrices of different types, i.e. having chemical-physical characteristics, such as humidity, granulometry, calorific value, different .

The plant for converting carbonaceous matrices, particularly for the production of energy, thus conceived is susceptible of numerous modifications and variations, all of which are within the scope of the inventive concept.

Furthermore, all the details can be replaced by other technically equivalent elements.

In practice, the materials employed, so long as compatible with the specific use, as well as the contingent shapes and dimensions, may be any according to requirements.

Claims (13)

R I V E N D I C A Z I O N I 1. Carbon matrix conversion plant (1), particularly for the production of energy, comprising a carbon matrix conversion station, which comprises: - a reaction chamber (3) where a synthesis gas (20) is extracted from a carbonaceous matrix, - a combustion chamber (4) capable of generating a heating vector (40) for heating said chamber reaction (3), e - an expansion tower (5), where said synthesis gas (20) is separated from solid products (21), and comprising a filtering and cooling station (7, 8, 9) of said synthesis gas (20) leaving said expansion tower (5), characterized in that said reaction chamber (3) comprises an internal tubular element (30) adapted to rotate with respect to a longitudinal rotation axis (31), and an external tubular element (300) concentric to said internal tubular element (30), said internal tubular element (30) comprising, on the external lateral surface (32 ), a plurality of blades (33, 34) defining, along at least a longitudinal portion of said external lateral surface (32) of said internal tubular element (30), a plurality of channels (35) for advancement, along said chamber reaction (3), of said carbonaceous matrix and of said synthesis gas (20) forming from said carbonaceous matrix, said heating thermal vector (40) flowing inside said internal tubular element (30). 2. Plant for the conversion of carbonaceous matrices (1), according to claim 1, characterized in that the direction of advancement, along said reaction chamber (3), of said carbonaceous matrix and of said synthesis gas (20) being formed from said carbonaceous matrix, it is opposite to the longitudinal flow direction of said thermal vector (40) inside said internal tubular element (30). 3. Plant for converting carbonaceous matrices (1), according to claims 1 or 2, characterized in that said channels (35) are wound in a spiral around said internal tubular element (30), the rotation of said internal tubular element ( 30) and of said blades (33, 34) causing the advancement, along said reaction chamber (3), of said carbonaceous matrix and of said synthesis gas (20) forming from said carbonaceous matrix. 4. Carbon matrix conversion plant (1), characterized in that the rotation axis (31) of said internal tubular element (30) is inclined with respect to a horizontal direction, the rotation of said internal tubular element (30 ) and of said blades (33, 34) causing the advancement, along said reaction chamber (3), of said carbonaceous matrix. 5. Plant for converting carbonaceous matrices (1), characterized in that said external tubular element (300) is able to rotate together with said internal tubular element (30) and said blades (33, 34). 6. Plant for converting carbonaceous matrices (1), according to one or more of the preceding claims, characterized in that said expansion tower (5) comprises means for the injection of air or oxygen (50, 51, 52) for raising the temperature of said synthesis gas (20). 7. Carbon matrix conversion plant (1), according to one or more of the preceding claims, characterized in that the internal environment of said reaction chamber (3) and expansion tower (5) is in constant depression. 8. Plant for converting carbonaceous matrices (1), according to one or more of the preceding claims, characterized in that it comprises a by-pass station (6) suitable for collecting the synthesis gas (20) coming out of said expansion (5) and burning it in the atmosphere during the start-up phase of said plant (1). 9. Carbon matrix conversion plant (1), according to one or more of the preceding claims, characterized in that said filtration and cooling station (7, 8, 9) comprises: - at least one cyclone (70, 71) adapted to abate the particulate present in said synthesis gas (20); - at least one bag filter (80) adapted to purify said synthesis gas (20) from microparticulate present in said synthesis gas (20); - at least one heat exchange battery (90, 91) suitable for lowering the temperature of said synthesis gas (20). 10. Conversion process of carbonaceous matrices, comprising the steps of: - extracting synthesis gas (20) from a carbonaceous matrix, in a reaction chamber (3); generating a heating thermal vector (40), for heating said reaction chamber (3), - separating said synthesis gas (20) from solid products (21) in an expansion tower (5), - filtering and cooling said synthesis gas (20) leaving said expansion tower (5), characterized in that, said step of extracting synthesis gas (20) from said carbonaceous matrix, comprises the steps of: - starting from said reaction chamber (3) comprising an internal tubular element (30) able to rotate with respect to a longitudinal rotation axis (31), and an external tubular element (300) concentric to said internal tubular element (30) , said internal tubular element (30) comprising, on the external lateral surface (32), a plurality of blades (33, 34), defining, along at least a longitudinal portion of said external lateral surface (32) of said internal tubular element (30 ), a plurality of channels (35), advance said carbonaceous matrix and said synthesis gas (20) in formation from said carbonaceous matrix along said channels (35); - making said heating thermal vector (40) slide inside said internal tubular element (30). 11. Reaction chamber (3) for the conversion of carbonaceous matrices, characterized in that it comprises an internal tubular element (30) able to rotate with respect to a longitudinal rotation axis (31), and a concentric external tubular element (300) to said internal tubular element (30), said internal tubular element (30) comprising, on the external lateral surface (32), a plurality of blades (33, 34) defining along at least a longitudinal portion of said external lateral surface (32) of said internal tubular element (30), a plurality of channels (35) for the advancement, along said reaction chamber (3), of a carbonaceous matrix and of a synthesis gas (20) forming from said carbonaceous matrix, called internal tubular element (30) being able to contain a thermal vector (40) for heating said reaction chamber (3). 12. Filtration and cooling station (7, 8, 9), for the filtration and cooling of a synthesis gas (20), characterized by the fact of comprising: - at least one cyclone (70, 71) adapted to abate the particulate present in said synthesis gas (20); - at least one bag filter (80) adapted to purify said synthesis gas (20) from microparticulate present in said synthesis gas (20); - at least one heat exchange battery (90, 91) suitable for lowering the temperature of said synthesis gas (20). 13. Filtration and cooling station (7, 8, 9), for the filtration and cooling of a synthesis gas (20), according to claim 12, characterized in that said synthesis gas (20) is subject to a first temperature drop in said at least one cyclone (70, 71), at a second temperature drop in said bag filter (80) and at a third temperature drop in said at least one heat exchange battery (90, 91) .