Plant and process for the treatment of waste by catalytic conversion into combustible fluids

Abstract

A plant (1) for the treatment of waste by catalytic conversion into combustible fluids, comprising: - a reactor (2) for containing a reaction mixture (MR) formed from waste, a catalyst, and a carrier liquid (LV), the reactor (2) having a head provided with an outlet through-opening (3) for an ascending gaseous stream composed of hydrocarbons, water, and carrier liquid (LV), which separates from the reaction mixture (MR); - a recirculation circuit (4) for the reaction mixture (MR) within the reactor, the recirculation circuit comprising a recirculation pump (5) and a heat exchanger (6); - a carrier liquid recovery circuit (7) configured for the continuous withdrawal from the recirculation circuit (4) of a portion of the reaction mixture (MR), and for the subsequent separation of solid reaction products, inert materials, and spent catalyst from the carrier liquid (LV); the plant further comprises a first reflux column (8), a condensation and separation unit (9), and a second distillation column (10), wherein the first reflux column (8) is mounted on the head of the reactor (2) and in fluid communication with the outlet through-opening (3) for separating the gaseous stream into a first gaseous component (1G) containing water and more volatile fractions of the carrier liquid (LV) and hydrocarbons, and a first condensed liquid component (IL) returned to the reactor, containing less volatile fractions of the carrier liquid (LV) and hydrocarbons; wherein the condensation and separation unit (9) is configured to condense the first gaseous component (1G) into a second liquid component (2L) and separate the second liquid component (2L) into a third liquid component (3L) based on hydrocarbons and carrier liquid (LV), and a fourth liquid component (4L) based on water; and wherein the second distillation column (10) is configured to separate the third liquid component (3L) into a second gaseous component (2G) based on hydrocarbons and a fifth liquid component (5L) based on carrier liquid (LV).

Description

[0001] PLANT AND PROCESS FOR THE TREATMENT OF WASTE BY CATALYTIC CONVERSION INTO COMBUSTIBLE FLUIDS

[0002] DESCRIPTION

[0003] The present invention relates to a plant for waste treatment through catalytic conversion into combustible fluids.

[0004] The disposal of the enormous volume of waste produced represents a significant issue, as it is not feasible to send all generated waste to landfills.

[0005] To reduce the amount of waste sent to landfills, dedicated waste incineration plants (commonly referred to as incinerators or waste-to-energy plants) have long been used. These plants allow for the elimination of waste through a high-temperature combustion process (incineration), which results in a gaseous effluent, ashes, and dust as final products.

[0006] In next-generation incineration plants, the heat produced during waste combustion is recovered and used to produce steam, which is then utilized to generate electricity or as a heat carrier (e.g., for district heating). While incineration plants have significantly reduced the volume of waste destined for landfills, they have the major drawback of emitting highly polluting compounds into the atmosphere (such as dioxins).

[0007] To overcome this drawback, treatment plants using non-combustion technologies have been proposed, which involve the thermochemical decomposition of waste, producing as final products a gas, a combustible liquid, and a solid with residual calorific value.

[0008] In such plants, waste is mixed with a carrier fluid and a reaction catalyst and heated (typically to temperatures below 400°C) in the absence of oxygen, in order to avoid any combustion (and therefore the emission of polluting gaseous compounds).

[0009] Generally, these plants use a reactor associated with a recirculating evaporator. The waste treated in these systems is typically hydrocarbon-based. Patent DE10049377 is an excellent example of such a type of plant. The reactor and its connecting ducts are filled with diathermic oil or heavy fuel oil mixed with a catalyst.

[0010] In the past, to supply the dense fuel oil-waste mixture with the energy required for the decomposition chemical reaction, a burner was placed next to the reactor, associated with a combustion chamber for the solid residue obtained as a by-product of the chemical reaction. Although this proposed solution was conceptually valid, it was not without its drawbacks.

[0011] In particular, heating the mixture using the combustion fumes from the solid residue, a by-product of the reaction, rapidly caused deposits and encrustations on the tube bundles, drastically reducing the heat exchanger’s efficiency and increasing the plant’s operating costs. The issue described above was eventually addressed, as explained in several patents such as EP 1538191 Bl and EP 2113017 Al, through the development of a plant where the heating of the heavy fuel oil-waste mixture is achieved by converting kinetic energy into thermal energy (friction) via a mechanical agitator or a pump-turbine designed to generate a counterflow relative to the pumped flow of the heavy fuel oil-waste mixture. This counterflow, through friction, leads to the heating of the mixture.

[0012] However, the systems described in the aforementioned patents present significant drawbacks, such as frequent leaks from the pumping devices — typically centrifugal pumps — and inefficiencies in systems used to separate the carrier fluid from the various hydrocarbon components obtained at the end of the reaction.

[0013] The leakage issues in the pumping devices were largely resolved by patent ITVR20110169A1, in which the pump in the recirculation circuit connected to the reactor includes a magnetically driven centrifugal pump.

[0014] This configuration, which lacks mechanical drive elements, ensures sealing integrity with clear advantages from both a construction and operational standpoint, leading to a significant increase in efficiency and a reduction in losses and energy consumption. In that patent, the systems for separating the carrier fluid and the various hydrocarbon components obtained at the end of the reaction generally consist of a single distillation column with trays and bubble caps positioned directly at the top of the reactor.

[0015] While this column effectively separates the carrier fluid and the various hydrocarbon components resulting from the reaction, it does so at the cost of significant operational difficulty and energy consumption.

[0016] The technical objective of the present invention is therefore to provide a plant for the treatment of waste through catalytic conversion into combustible fluids that eliminates the technical drawbacks of the known art. Within this technical objective, one aim of the invention is to provide a plant capable of effectively separating the carrier fluid and the various hydrocarbon components obtained at the end of the reaction in a simple yet accurate manner, with the lowest possible energy consumption.

[0017] The technical objective, as well as these and other aims, are achieved according to the present invention by providing a plant for the treatment of waste through catalytic conversion into combustible fluids, comprising:

[0018] • a reactor for containing a reaction mixture formed from said waste, a catalyst, and a carrier liquid, said reactor having a head equipped with an outlet through-opening for an ascending gaseous stream, composed of hydrocarbons, water, and carrier liquid, which separates from said reaction mixture; » a recirculation circuit for the reaction mixture within the reactor, said recirculation circuit comprising a recirculation pump and a heat exchanger;

[0019] • a carrier liquid recovery circuit configured for the continuous withdrawal, from said recirculation circuit, of a portion of said reaction mixture, and for the subsequent separation of solid reaction products, inert materials, and spent catalyst from said carrier liquid; characterized by the inclusion of a first reflux column, a condensation and separation unit, and a second distillation column, wherein said first reflux column is mounted on the head of said reactor and in fluid communication with said outlet through-opening, for the separation of said gaseous stream into a first gaseous component containing water and the more volatile fractions of the carrier liquid and hydrocarbons, and a first condensed liquid component reintroduced into the reactor containing the less volatile fractions of the carrier liquid and hydrocarbons; wherein said condensation and separation unit is configured to condense the first gaseous component into a second liquid component and to separate the second liquid component into a third liquid component based on hydrocarbons and carrier liquid, and a fourth liquid component based on water; and wherein said second distillation column is configured to separate said third liquid component into a second gaseous component based on hydrocarbons and a fifth liquid component based on the carrier liquid.

[0020] The present invention also discloses a process for the treatment of waste comprising car fluff and / or tire granulate and / or Plasmix, through catalytic conversion into combustible fluids, comprising the following steps: forming, in a reactor, a reaction mixture consisting of said waste, a catalyst, and a carrier liquid including diathermic or mineral oil; separating from said reaction mixture an ascending gaseous stream composed of hydrocarbons, water, and carrier liquid, exiting through a through-opening in the head of said reactor; - recirculating the reaction mixture in a recirculation circuit within the reactor, said recirculation circuit comprising a recirculation pump and a heat exchanger;

[0021] - recovering the carrier liquid in a carrier liquid recovery circuit, which continuously withdraws a portion of said reaction mixture from the recirculation circuit and subsequently separates solid reaction products, inert materials, and the spent catalyst from said carrier liquid; in a first reflux column mounted on the head of said reactor and in fluid communication with said outlet through-opening, separating said gaseous stream into a first gaseous component containing water and the more volatile fractions of the carrier liquid and hydrocarbons, and a first condensed liquid component reintroduced into the reactor containing the less volatile fractions of the carrier liquid and hydrocarbons; in a condensation and separation unit, condensing the first gaseous component into a second liquid component and separating the second liquid component into a third liquid component based on hydrocarbons and carrier liquid, and a fourth liquid component based on water; in a second distillation column, separating said third liquid component into a second gaseous component based on hydrocarbons and a fifth liquid component based on carrier liquid.

[0022] The division of the distillation process into a first distillation column and a second distillation column solves a series of important technical issues.

[0023] In fact, although there is continuous feed into the reactor, the amount of vapor produced by the reaction is not constant — neither in flow rate nor in hydrocarbon concentration — meaning that the feed to the first distillation column, which is positioned directly at the top of the reactor, is highly variable. This variability makes it difficult to manage the first distillation column in terms of maintaining stable thermal profiles and thus obtaining products that meet the required specifications.

[0024] The presence of water inside the reactor, produced by the reaction itself, generates a steam flow which, although small, tends to create instability within the column. Hence the need to separate the water before it enters the second distillation column.

[0025] Stabilizing the operation of the second distillation column by separating it from the reactor allows for intermediate liquid withdrawals from the column, enabling the lateral extraction of different hydrocarbons (gasoline, kerosene, and diesel). Other features of the present invention are further defined in the subsequent claims. Additional features and advantages of the invention will become more apparent from the description of a preferred, though not exclusive, embodiment of the plant according to the invention, provided by way of example and not limitation in the accompanying drawings, in which: Figure 1 shows the schematic flow diagram of the plant.

[0026] With reference to the figures mentioned, a plant is shown and generally indicated by reference number 1.

[0027] The plant 1, for the treatment of waste through catalytic conversion into combustible fluids, is configured to typically treat waste such as: car fluff, tire granulate, Plasmix (i.e., mixed plastic waste), as well as other non-metallic waste from scrapped vehicles, and also for the treatment of residual biomass from agriculture, livestock, and forestry.

[0028] Before being introduced into the plant, the waste is processed to remove all metallic residues and retain only the components chemically relevant to the process.

[0029] Therefore, only ground solid waste R is fed into the plant.

[0030] The plant 1 comprises a reactor 2, a recirculation circuit 4, and a recovery circuit 7. The reactor 2 is configured to contain a reaction mixture MR made up of waste, a catalyst, and a carrier liquid LV.

[0031] Inside the reactor, the chemical reaction occurs that initiates the transformation of the input waste into synthetic solid, liquid, and gaseous fuels, typically hydrocarbons.

[0032] The reactor 2 features a head equipped with an outlet through-opening 3 for an ascending gaseous stream, composed of hydrocarbons, water, and carrier liquid LV, which separates from the reaction mixture MR as a result of the aforementioned chemical reaction.

[0033] The recirculation circuit 4 for the reaction mixture MR within the reactor includes a recirculation pump 5 and a heat exchanger 6, which brings the reaction mixture MR to the activation temperature of the aforementioned chemical reaction. To prevent liquid leakage to the outside, the recirculation pump 5 is a magnetically driven centrifugal pump.

[0034] The heat exchanger 6 of the recirculation circuit 4 for the reaction mixture MR in the reactor is positioned vertically, in order to greatly reduce issues related to the deposition of inert and metallic components — residues that may have escaped the initial waste preparation — inside the exchanger itself.

[0035] At the head of the reactor 2, offset from the outlet through-opening 3, there is an inlet opening 19 for the recirculated reaction mixture MR.

[0036] The carrier liquid recovery circuit 7 is configured for the continuous withdrawal from the recirculation circuit 4 of a portion of the reaction mixture MR, and for the subsequent separation of solid reaction products, inert materials, and the spent catalyst from the carrier liquid LV. The carrier liquid recovery circuit 7 includes a tank 13 and a dryer 14 for the production of carbon C through the drying of carbonaceous residues.

[0037] The dryer 14 includes a continuous thin- film evaporator for the carrier liquid LV.

[0038] This continuous thin-film evaporator is positioned horizontally, in such a way as to make it more efficient.

[0039] The carrier liquid recovery circuit 7 also includes, downstream of the dryer 14, a thermal refinement unit 15 for the carbon C discharged from the dryer 14, in order to obtain carbon black CN.

[0040] The plant 1 further includes a first reflux column 8, a condensation and separation unit 9, and a second distillation column 10.

[0041] The first reflux column 8 is mounted on the head of the reactor 2, and is in fluid communication with the outlet through-opening 3.

[0042] The first reflux column 8 is configured to separate the gaseous stream into a first gaseous component 1G, containing water and the more volatile fractions of the carrier liquid LV and hydrocarbons, and a first condensed liquid component IL, which is returned by gravity into the reactor and contains the less volatile fractions of the carrier liquid LV and hydrocarbons.

[0043] The condensation and separation unit 9 is configured to condense the first gaseous component 1G into a second liquid component 2L.

[0044] The condensation and separation unit 9 specifically comprises a heat exchanger 31 that condenses the first gaseous component 1G, and a decanter 18 equipped with a baffle system to separate the second liquid component 2L into a third liquid component 3L, based on hydrocarbons and carrier liquid LV, and a fourth liquid component 4L, based on water.

[0045] The second distillation column 10 is configured to separate the third liquid component 3L into a second gaseous component 2G, based on hydrocarbons, and a fifth liquid component 5L, based on carrier liquid LV.

[0046] The second distillation column 10 further includes a bottom reboiler 11, a top reflux condenser 12, and a tray column.

[0047] In particular, the second distillation column 10 is of the tray type, using valve or bubble cap trays. The bottom reboiler 11 includes a pump 11a and a heat exchanger 1 lb, and ensures proper vapor generation within the second distillation column 10.

[0048] The top reflux condenser 12 includes a heat exchanger 12a and a storage tank 12b.

[0049] The plant 1 also includes a premixer 16 for the waste, catalyst, and carrier liquid LV, for the preparation of a heterogeneous solid-liquid mixture M to be fed into the reactor 2. The function of the premixer is to blend the waste and catalyst with the carrier liquid LV, to form the aforementioned heterogeneous solid-liquid mixture M.

[0050] If the heterogeneous solid-liquid mixture M did not contain the carrier liquid LV, the vapors ascending to the first column 8 would drag with them a portion of dry dust from the solid waste, with the risk of it adhering to and accumulating on the walls of the ducts, causing constrictions and blockages. By using the carrier liquid LV, the dust particles remain trapped within the liquid.

[0051] The premixer 16 includes screw conveyors or a magnetically driven pump, generically indicated as 17, for transferring the heterogeneous solid-liquid mixture M to the reactor 2. The carrier liquid recovery circuit 7 is connected to the premixer 16 to supply the recovered carrier liquid LV.

[0052] The plant 1 includes a first mechanical mixer 22 inside the premixer 16, a second mechanical mixer 23 inside the reactor 2, and a third mechanical mixer 24 inside the tank 13 of the carrier liquid LV recovery circuit 7.

[0053] It should be noted that a small continuous stream is withdrawn from the outlet of heat exchanger 6, which serves reactor 2, and is sent to tank 13, equipped with mixer 24. Necessarily, a portion — although small — of unreacted material from reactor 2 is thus transferred into tank 13.

[0054] Thanks to its volume, the presence of mixer 24, and its internal temperature, tank 13 allows this unreacted material to complete its reaction.

[0055] This ensures full utilization of the input material to the plant and avoids the presence of undesired products in dryer 14.

[0056] The carbon C exiting dryer 14 contains, in variable amounts depending on the feed material introduced into the plant, unreacted or partially reacted polymers — typically polyolefin polymers — whose intramolecular bonds are not cleaved under the thermal and catalytic conditions present in reactor 2, flash tank 13, and dryer 14.

[0057] As mentioned, the carbon C exiting dryer 14 is sent to the thermal refinement unit 15 for the production of carbon black CN.

[0058] A suitable temperature range has been identified for this operation, which consists of a second (purely thermal) depolymerization of the aforementioned polyolefin polymers. This temperature range lies between 450°C and 600°C, and preferably between 450°C and 500°C. Within this temperature range, the bond cleavage reaction in polyolefin polymers is triggered. Unlike the reactions that occur in reactor 2, and possibly in tank 13 and dryer 14, this cleavage reaction is exclusively radical in nature.

[0059] In contrast, the reactions in reactor 2, tank 13, and dryer 14 are predominantly catalytic and only marginally radical, the latter requiring a minimum temperature of approximately 450°C.

[0060] The difference between the two reaction types lies in how the two bonding electrons are distributed between the atoms involved.

[0061] The radical reaction leads to homolytic bond cleavage, where each atom retains one electron, forming two free radicals. This occurs in purely covalent bonds such as C-C.

[0062] The catalytic reaction leads to heterolytic bond cleavage, where both electrons are retained by the more electronegative atom, resulting in the formation of a negative ion and a positive ion (the atom from which the electron has been "stripped"). This occurs in polar covalent bonds such as C-O, C-N, C-S, and C-Cl.

[0063] The catalytic reaction therefore requires the presence of polar covalent bonds, that is, bonds between a carbon atom and a different, typically more electronegative atom. In this case, a carbocation and an anion are formed, and through the recombination of these ionic fragments, the molecules observed in the liquid and gas analyses are derived.

[0064] The presence of polyolefins in the refinement unit 15, whose polymer chain bonds are essentially pure covalent C-C bonds, is due to the presence of unreacted polyolefins in the carbon C exiting the dryer 14.

[0065] The residual polyolefins are depolymerized in the refinement unit 15 both to increase the yield of conversion into liquid and gaseous products from the input feed material, and especially to obtain a carbon black CN free from such components — thus more easily micronized to the particle sizes required by the market, typically below 100 microns, and down to 10 microns for the most specialized carbon black applications. The plant 1 includes one or more vacuum generation units 20, and downstream of these, a scrubber 21 for the basic washing of non-condensable gases coming from the first gaseous component 1G, the second gaseous component 2G, and the carrier liquid LV recovery circuit 7.

[0066] Specifically, the plant 1 includes a first vacuum generation unit 20, downstream of the heat exchanger 12a of the top reflux condenser 12, for drawing non-condensable gases from the second gaseous component 2G, and a second vacuum generation unit 20, downstream of a heat exchanger 25 belonging to the recovery circuit 7 of the carrier liquid LV, for drawing non-condensable gases exiting from the recovery circuit 7.

[0067] Finally, the plant 1 includes a condenser 26 connected at the inlet to the outlet of the non- condensable gases from the first gaseous component 1G and from both vacuum generation units 20.

[0068] The condenser 26 is connected at the outlet to the storage tank 12b of the top reflux condenser 12 for the recovery of the condensed liquid component, and to the scrubber 21 for the passage of the non-condensed gaseous component.

[0069] As shown, the condenser 26 may also be connected to a chilled water generation unit 33.

[0070] Finally, the outlet of the scrubber 21 is connected to a process gas compressor 27 for the discharge of gaseous hydrocarbons.

[0071] The operation of the plant 1 according to the invention is evident from what has been described and illustrated, and in particular, it is substantially as follows.

[0072] The ground solid waste R, free from metallic components, enters the premixer 16 together with the catalyst, pushed in by a screw conveyor 28.

[0073] Through a second inlet, the carrier liquid LV — heated and coming from the recovery circuit 7 — also enters the premixer 16.

[0074] This recovered carrier liquid LV enters the premixer 16, preheated by heat exchanger 30, to maintain, for example, a temperature of approximately 200°C inside the premixer 16. Through a third inlet, fresh carrier liquid LV is introduced into the premixer 16 to compensate for any losses in the carrier liquid circuit.

[0075] The carrier liquid LV normally used in this application is diathermic or mineral oil.

[0076] At the heating temperature provided by the hot oil, moisture in the waste evaporates along with light hydrocarbons present in the fresh oil, and the vapors are conveyed to the condensation and separation unit 9, where they are condensed by indirect cooling with water.

[0077] The liquid is then sent to the decanter 18, where gravity separates the hydrocarbons belonging to the third liquid component 3L from the water belonging to the fourth liquid component 4L, which is extracted.

[0078] Inside the premixer 16, the heterogeneous solid-liquid mixture M is blended by the first mixer 22 and then sent to the reactor 2.

[0079] Inside reactor 2, the reaction mixture MR is heated by heat exchanger 6 belonging to the recirculation circuit 4 and mixed by the second mechanical mixer 23.

[0080] The catalytic reaction takes place in reactor 2, transforming the waste into hydrocarbons.

[0081] From the reaction mixture MR heated by heat exchanger 6, an ascending gaseous stream is gradually formed, composed of hydrocarbons, water, and carrier liquid LV, which separates from the mixture and exits reactor 2 through the outlet opening 3.

[0082] After passing through opening 3, the ascending gaseous stream enters the first reflux column 8, which separates the first gaseous component 1G and the first condensed liquid component IL. The first gaseous component 1G, containing water and the more volatile fractions of the carrier liquid LV and hydrocarbons, rises toward the condensation and separation unit 9. The first liquid component IL is returned by gravity to the reactor and contains the less volatile fractions of the carrier liquid LV and hydrocarbons.

[0083] The condensation and separation unit 9 condenses part of the first gaseous component 1G into a second liquid component 2L, and separates the non-condensable gases from component 1G. The second liquid component 2L is sent to the decanter 18 to separate the third liquid component 3L based on hydrocarbons and carrier liquid LV from the fourth liquid component 4L based on water, which is extracted and stored in tank 32.

[0084] The third liquid component 3L is sent to the second distillation column 10, where it is separated into the fifth liquid component 5L and the second gaseous component 2G. The bottom reboiler 11 maintains the second distillation column 10 at the temperature needed to ensure proper vapor production.

[0085] The fifth liquid component 5L is sent to the recovery circuit 7, which also receives part of the reaction mixture MR.

[0086] The recovery circuit 7 separates: carbon C (CHEMCARBON); carbon black CN; the carrier liquid LV which is stored in tank 29, reheated by heat exchanger 30, and returned to premixer 16; and non-condensable gases, which are sent to the vacuum generation unit 20.

[0087] The second gaseous component 2G is sent to the top reflux condenser 12, which condenses and separates the high-boiling hydrocarbon component as liquid (CHEMFUEL), part of which is returned to the top of distillation column 10 as reflux.

[0088] It also separates the low-boiling, non-condensable gas component, which is sent to the vacuum generation unit 20.

[0089] The gases from the first gaseous component 1G and those from the vacuum generation units 20 are partially condensed and returned to the reflux condenser 12.

[0090] The remaining non-condensable gases are sent to the scrubber 21 and then to the process gas compressor 27, where the gaseous hydrocarbons (CHEMGAS) are finally discharged.

[0091] It should be noted that the thermal refinement unit 15 produces mainly gaseous products through depolymerization of polyolefins, which are extracted by compressor 27 and incorporated into the CHEMGAS stream.

[0092] Thanks to the refinement unit 15, it is also possible to improve the plant’s energy efficiency, since increasing the amount of CHEMGAS sent for thermal recovery reduces the need to supply natural gas from the distribution network.

[0093] In practice, it has been observed that the plant 1, according to the invention, is particularly advantageous, as it allows for systematic, high-yield treatment of waste that would otherwise be landfilled, through catalytic conversion into combustible fluids and carbonaceous solids.

[0094] Moreover, at the end of the reaction, the plant 1 has the advantage of being able to efficiently separate the carrier fluid and the various hydrocarbon components obtained from the reaction.

[0095] The plant 1 as conceived is subject to numerous modifications and variations, all of which fall within the scope of the inventive concept.

[0096] In addition, all the details may be replaced with technically equivalent elements.

[0097] In practice, the materials used — as well as the dimensions — may be of any type, depending on specific requirements and the state of the art.

Claims

CLAIMS1. Plant (1) for waste treatment by catalytic conversion into combustible fluids, comprising:• a reactor (2) for containing a reaction mixture (MR) formed from said waste, a catalyst, and a carrier liquid (LV), said reactor (2) having a head provided with an outlet through-opening (3) for an ascending gaseous stream based on hydrocarbons, water, and carrier liquid (LV), which separates from said reaction mixture (MR);• a recirculation circuit (4) for the reaction mixture (MR) in the reactor, said recirculation circuit comprising a recirculation pump (5) and a heat exchanger (6);• a carrier liquid (LV) recovery circuit (7) configured to continuously withdraw a portion of said reaction mixture (MR) from the recirculation circuit (4), and to subsequently separate solid reaction products, inert materials, and spent catalyst from said carrier liquid (LV); characterized by comprising a first reflux column (8), a condensation and separation unit (9), and a second distillation column (10), wherein said first reflux column (8) is mounted on the head of said reactor (2) and in fluid communication with said outlet through-opening (3) for separating said gaseous stream into a first gaseous component (1G) containing water and more volatile fractions of carrier liquid (LV) and hydrocarbons, and a first condensed liquid component (IL) returned to the reactor and containing less volatile fractions of carrier liquid (LV) and hydrocarbons; wherein said condensation and separation unit (9) is configured to condense the first gaseous component (1G) into a second liquid component (2L) and separate said second liquid component(2L) into a third liquid component (3L) based on hydrocarbons and carrier liquid (LV) and a fourth liquid component (4L) based on water; and wherein said second distillation column (10) is configured to separate said third liquid component (3L) into a second gaseous component (2G) based on hydrocarbons and a fifth liquid component (5L) based on carrier liquid (LV).

2. Plant (1) according to claim 1, characterized in that said second distillation column (10) comprises a bottom reboiler (11) and a top reflux condenser (12).

3. Plant (1) according to any of the preceding claims, characterized in that said heat exchanger (6) of the recirculation circuit (4) is a vertical heat exchanger.

4. Plant (1) according to any of the preceding claims, characterized in that said carrier liquid recovery circuit (7) comprises a tank (13) and a dryer (14) for producing carbon from the drying of carbonaceous residues, said dryer (14) comprising a continuous thin-film evaporator for the carrier liquid (LV).

5. Plant (1) according to the preceding claim, characterized in that said continuous thin-film evaporator is a horizontal evaporator.

6. Plant (1) according to any of claims 4 or 5, characterized in that said carrier liquid recovery circuit (7) further comprises, downstream of said dryer (14), a thermal refinement unit (15) for refining the carbon (C) exiting said dryer (14) and obtaining carbon black (CN).

7. Plant (1) according to any of the preceding claims, characterized by comprising a premixer (16) for the waste, the catalyst, and the carrier liquid (LV), for preparing a heterogeneous solidliquid mixture (M) to be introduced into the reactor (2).

8. Plant (1) according to any of the preceding claims, characterized in that said second distillation column (10) comprises a valve tray or bubble cap tray column.

9. Plant (1) according to any of the preceding claims, characterized in that at the head of the reactor (2), offset from said outlet through-opening (3), an inlet opening (19) is provided for the recirculated reaction mixture (MR).

10. Plant (1) according to any of claims 7 to 9, characterized by comprising a first mechanical mixer (22) inside the premixer (16), a second mechanical mixer (23) inside the reactor (2), and a third mechanical mixer (24) inside the tank (13) of the carrier liquid recovery circuit (7).

11. Process for the treatment of waste, including car fluff and / or tire granulate and / or Plasmix, by catalytic conversion into combustible fluids, comprising the following steps:• forming, in a reactor (2), a reaction mixture (MR) consisting of said waste, a catalyst, and a carrier liquid (LV) including diathermic or mineral oil; » separating from said reaction mixture (MR) an ascending gaseous stream based on hydrocarbons, water, and carrier liquid (LV), exiting from an outlet through-opening (3) in the head of said reactor (2);• recirculating the reaction mixture (MR) in a recirculation circuit (4) comprising a pump (5) and a heat exchanger (6); » recovering the carrier liquid (LV) in a recovery circuit (7) that continuously withdraws a portion of said reaction mixture (MR) from said recirculation circuit (4) and separates solid reaction products, inert materials, and spent catalyst from the carrier liquid (LV);• in a first reflux column (8) mounted on the head of said reactor (2) and in fluid communication with said outlet (3), separating said gaseous stream into a first gaseous component (1G) containing water and more volatile fractions of carrier liquid (LV) and hydrocarbons, and a first condensed liquid component (IL) returned to the reactor and containing the less volatile fractions;• in a condensation and separation unit (9), condensing the first gaseous component (1G) into a second liquid component (2L) and separating said second liquid into a third liquid component (3L) based on hydrocarbons and carrier liquid (LV), and a fourth liquid component (4L) based on water;» in a second distillation column (10), separating said third liquid component (3L) into a second gaseous component (2G) based on hydrocarbons and a fifth liquid component (5L) based on carrier liquid (LV).

12. Process according to the preceding claim, characterized by comprising the step of:• in a dryer (14) of said recovery circuit (7), comprising a continuous thin- film evaporator, producing carbon by drying carbonaceous residues.

13. Process according to the preceding claim, characterized by comprising the step of: in a thermal refinement unit (15) of said recovery circuit (7), arranged downstream of said dryer (14), obtaining carbon black (CN) through the thermal refinement of said carbon (C) exiting the dryer (14).

14. Process according to the preceding claim, characterized in that said thermal refinement of carbon (C) takes place at a temperature between 450°C and 600°C to depolymerize unreacted polyolefins present in the carbon (C) exiting said dryer (14).

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