Apparatus and process for separation of components of a multiphase hydrocarbon stream

Description

1 / 18 APPARATUS AND PROCESS FOR SEPARATING COMPONENTS FROM A MULTIPHASE HYDROCARBON STREAM

[001] The present invention relates to an apparatus and a process for separating components of a multi-phase hydrocarbon stream.

[002] Hydrocarbon cracking processes generally involve the decomposition of longer-chain hydrocarbons into shorter-chain hydrocarbons, usually at moderate or high temperatures, for example, between 400 and 600°C (thermal cracking), and / or in the presence of catalysts (catalytic cracking). A particularly interesting application of cracking processes is the depolymerization of plastic materials, which is used in the recycling of plastic waste.

[003] Cracking processes typically result in complex mixtures of hydrocarbons that need to be at least partially separated. These mixtures, obtained from a cracking reactor, are usually multi-phase systems. For example, the vapor phase may contain desired cracked hydrocarbons, the liquid phase may contain hydrocarbons that have not yet been sufficiently cracked, and the solid phase may include coke particles. In addition, impurities may be present, particularly with regard to the recycling of plastic waste. Solid impurities may include, in addition to coke particles, for example, aluminum dust, fillers, or ash. Vapor impurities may include, for example, certain organophosphorus components commonly used in plastic materials.

[004] International patent application WO 2020 / 168062 A1 describes a process for removing coke and tar from a steam cracking furnace effluent, wherein a furnace effluent Petition 870260022828, dated 12 / 03 / 2026, page 10 / 65 2 / 18 rapidly cooled is introduced into a centrifugal separator, where a vapor product and a centrifugal separator bottom product, comprising at least a portion of coke and / or tar, are separated.

[005] US Patent 2,776,931 describes a process and apparatus for rapidly cooling and separating hot effluent vapors from a coking operation, wherein the hot effluent vapors are rapidly cooled, thereby liquefying certain high-boiling-point contaminants, and then promoting the separation, in a cyclonic separation zone, of liquids and solids from the remaining rapidly cooled vapors.

[006] US Patent 2,927,890 describes a process involving the separation and rapid cooling of gaseous products from a thermal conversion of a residual petroleum-based oil feed, wherein a rapidly cooled stream is passed to a cyclonic separation zone to separate non-condensed vapors from entrained solids and a liquid stream, and wherein the liquid stream is then separated from the solids.

[007] It is an object of the present invention to alleviate at least one or more of the deficiencies of the prior art. In particular, it is an object of the present invention to provide an apparatus and a process that provide, at least partially, a separation of vaporous, liquid and solid components of a multi-phase hydrocarbon stream in a single piece of equipment. Furthermore, it is another object of the present invention to provide an apparatus and a process that provide a more efficient removal of impurities from a multi-phase hydrocarbon stream, in particular, from a multi-phase hydrocarbon stream obtained from the depolymerization of plastic materials.

[008] For this purpose, the present invention provides an apparatus Petition 870260022828, dated 12 / 03 / 2026, page 11 / 65 3 / 18 for separating the components of a multi-phase hydrocarbon stream, the apparatus comprising: - an outer container having a top end comprising a top outlet, a bottom end comprising a bottom outlet, with a longitudinal axis extending between the top end and the bottom end, and an outer container body disposed between the top end and the bottom end and having an inner volume of the outer container, in fluid communication with the top outlet and the bottom outlet, wherein the outer container body comprises: - a first section, comprising a tangential inlet, arranged to introduce the multi-phase hydrocarbon stream tangentially into the internal volume of the outer vessel to create a vortex flow; and - a second section positioned closer to the bottom end than the first section, wherein the internal volume of the outer container has a smaller cross-sectional circumference in the second section than in the first section; - an inner container disposed within the body of the outer container, said inner container comprising: - a body of the inner container having an inner volume of the inner container; and - an internal bottom inlet oriented towards the bottom end of the outer container and communicating via fluid with the internal volume of the inner container and with the internal volume of the outer container; and - a through conduit communicating via fluid with the internal volume of the inner container and passing through the body of the outer container.

[009] In another aspect, the invention provides a process for Petition 870260022828, dated 12 / 03 / 2026, page 12 / 65 4 / 18 Separating the components of a multi-phase hydrocarbon stream in an apparatus according to the invention, the process comprising the steps of: - Introduce the multi-phase hydrocarbon stream, through the tangential inlet, into the internal volume of the outer vessel to create a vortex flow, whereby a vapor product is separated from the hydrocarbon stream and transported to the top outlet; - recover said product in vapor form from the top outlet; - to transport the hydrocarbon stream from the first section to the second section, thereby increasing the tangential velocity of the vortex flow, in which the hydrocarbon stream is separated into a product stream enriched with solids and a product stream with reduced solids, where the product stream enriched with solids is transported to the bottom outlet; - recover the solids-enriched product stream from the bottom outlet; - To transport the reduced solids product stream into the inner volume of the inner container through the bottom inlet of the inner container; and - to recover the product stream with reduced solids volume from the inner container through the through conduit.

[0010] The inventive apparatus and process provide at least partial separation of vaporous, liquid, and solid components from a multi-phase hydrocarbon stream in a single piece of equipment. With respect to the present invention, the term "multi-phase" refers to the presence of more than one phase of matter. Preferably, the multi-phase hydrocarbon stream comprises at least three phases, particularly including vaporous, liquid, and solid components. The first section of the inventive apparatus advantageously provides vapor separation from liquids and solids; Petition 870260022828, dated 12 / 03 / 2026, page 13 / 65 5 / 18 The second section advantageously allows for the separation of the liquid and solid mixture into a product stream enriched with solids and a product stream with reduced solids. Conducting these separation processes in a single piece of equipment reduces costs and complexity while simultaneously increasing efficiency. Furthermore, piping and control valves, which might otherwise be necessary for connecting the separate separation devices, can be avoided, resulting in greater robustness and lower failure rates, for example, due to clogging.

[0011] In the inventive apparatus, the internal volume of the outer container has a smaller circumference in cross-section in the second section than in the first section of the outer container body. Unless otherwise indicated, the term cross-section, as used in this descriptive report, refers to an intersection with a plane that is substantially perpendicular to the longitudinal axis. Thus, the circumference in cross-section of the internal volume of the outer container refers to the circumference of the area of ​​the internal volume of the outer container in a plane in cross-section that is substantially perpendicular to the longitudinal axis of the outer container. The first section of the outer container body provides for the separation of vapors from liquids and solids, according to the principle of cyclonic separation.The solid and liquid components are pushed radially outwards towards the inner surface of the outer container body by a centrifugal force and continue to move axially towards the second section, while the vaporous components are pushed radially inwards and move axially upwards towards the top outlet. By providing a larger cross-sectional circumference in the first section, the axial velocity of the product vapor moving towards the top outlet is reduced, which advantageously reduces entrainment. Petition 870260022828, dated 12 / 03 / 2026, page 14 / 65 6 / 18 liquid droplets with the vapor, thus improving separation efficiency. At the same time, providing a smaller cross-sectional circumference in the second section allows for a higher tangential velocity of the vortex flow in the second section, which advantageously reduces residence time and thus the tendency to coking. Simultaneously, the higher tangential velocity in the second section provides greater centrifugal force and thus better separation efficiency in that section.

[0012] Preferably, the ratio of the circumference in cross-section of the internal volume of the outer container, in the second section, to the circumference in cross-section of the internal volume of the outer container, in the first section, is less than 0.95, preferably less than 0.9, particularly less than 0.8, more particularly less than 0.7, especially less than 0.6. It is especially preferred if said ratio is between 0.05 and 0.95, preferably between 0.1 and 0.9, particularly between 0.25 and 0.8, more particularly between 0.7 and 0.7, especially between 0.5 and 0.6.

[0013] Preferably, the internal volume of the outer container, in the first section, has a ratio of its length along the longitudinal axis to the diameter of its cross-sectional area between 0.2 and 5, preferably between 0.33 and 3, particularly between 0.5 and 2, more particularly between 0.75 and 1.8, especially between 1 and 1.4. In this regard, it is especially preferred if the internal volume of the outer container, in the first section, is substantially cylindrical.

[0014] Preferably, the internal volume of the outer container, in the second section, has a ratio of its length along the longitudinal axis to the diameter of its cross-sectional area between 0.4 and 10, preferably between 0.66 and 6, j, between 0.66 and 6, j, between 1 and 4, more particularly between 1.33 and 3, especially between 1.6 and 2.5. In this regard, it is especially preferred if the internal volume of Petition 870260022828, dated 12 / 03 / 2026, page 15 / 65 7 / 18 outer container, in the second section, is substantially cylindrical.

[0015] In a preferred embodiment, the apparatus further comprises a third section for connecting the first and second sections. Preferably, the internal volume of the outer container in said third section is substantially truncated conical.

[0016] In a preferred embodiment of the inventive process, the tangential velocity of the vortex flow, in the first section, is between 0.01 and 20 m / s, preferably between 0.05 and 10 m / s, particularly between 0.1 and 5 m / s, especially between 0.2 and 2.5 m / s.

[0017] It is further preferred if the tangential velocity of the vortex flow, in the second section, is between 0.05 and 10 m / s, preferably between 0.1 and 5 m / s, j, between 0.1 and 5 m / s, j, between 0.25 and 2.5 m / s, especially between 0.5 and 2 m / s.

[0018] In a preferred embodiment, the ratio of the tangential velocity of the vortex flow in the first section to the tangential velocity of the vortex flow in the second section is between 0.05 and 0.99, preferably between 0.1 and 0.95, particularly between 0.2 and 0.9, more particularly between 0.3 and 0.8, especially between 0.4 and 0.7.

[0019] In another preferred embodiment, the average residence time of the vortex flow, in the second section, is between 0.1 and 30 minutes, preferably between 0.2 and 10 minutes, particularly between 0.5 and 8 minutes, particularly between 0.8 and 6 minutes. Preferably, the average residence time is determined by CFD simulation.

[0020] The tangential inlet, located in the first section of the outer vessel body, is arranged to allow the creation of a vortex flow within the inner volume of the outer vessel when the multiphase hydrocarbon stream is introduced through said tangential inlet. A person skilled in the art is familiar with such arrangements, as they are commonly used in cyclone separators. Preferably, the tangential inlet is arranged Petition 870260022828, dated 12 / 03 / 2026, page 16 / 65 8 / 18 tangentially to the cross-sectional area of ​​the inner volume of the outer container, in a plane that is substantially perpendicular to the longitudinal axis.

[0021] In a preferred embodiment, the inventive apparatus further comprises a tangential conduit, communicating by fluid with the multi-phase hydrocarbon stream, preferably wherein the tangential conduit comprises a vaporization valve. Preferably, said tangential conduit is fluid-connected to a hydrocarbon cracking reactor. By providing a vaporization valve, vaporization evaporation of the hydrocarbon stream is permitted, wherein the hydrocarbon stream undergoes a reduction in pressure, and at least some of the components of the hydrocarbon stream pass from a liquid phase to a vapor phase.

[0022] With regard to the inventive apparatus, it is preferred if the ratio of the circumference in cross-section of the internal volume of the inner container to the circumference in cross-section of the internal volume of the outer container, in the second section, is at least 0.1, preferably at least 0.25, particularly at least 0.4, more particularly at least 0.5, especially at least 0.6. It is especially preferred if said ratio is between 0.1 and 0.99, preferably between 0.25 and 0.95, particularly between 0.4 and 0.9, more particularly between 0.5 and 0.85, especially between 0.6 and 0.8. A high ratio has the advantage that a greater proportion of the internal volume of the outer container is occupied by the body of the inner container, which promotes a greater tangential velocity of the vortex flow.This advantageously reduces the residence time and therefore the tendency to coking, and at the same time can lead to greater centrifugal force and thus better separation.

[0023] Preferably, the product stream enriched with Petition 870260022828, dated 12 / 03 / 2026, page 17 / 65 9 / 18 solids has a higher solids content than the current reduced solids product, preferably by at least 5%, particularly by at least 10%, more particularly by at least 20%, especially by at least 50%. Preferably, the solids content used in this descriptive report corresponds to the ash content. The ash content is preferably determined in accordance with ISO 6245:2001.

[0024] In a preferred embodiment, the inventive apparatus further comprises a cooling system, fluid-connected to the top outlet, wherein the cooling system is adapted to condense a portion of a product into vapor, which exits the internal volume of the outer container through the top outlet, and to transport the condensed portion of the product into vapor back to the internal volume of the outer container. Preferably, said cooling system comprises at least one spray nozzle. Similarly, in a preferred embodiment of the inventive process, said process further comprises the step of condensing a portion of the product into vapor, which exits the internal volume of the outer container through the top outlet, and transporting the condensed portion of the product into vapor back to the internal volume of the outer container.Preferably, said condensation is carried out by spraying a fluid onto the vapor product, wherein the temperature of said fluid is lower than the temperature of the vapor product; preferably, the temperature of said fluid is between 120°C and 350°C, particularly between 150°C and 300°C, especially between 180°C and 250°C. It is further preferred if said fluid is obtained by condensation and recycling of a portion of the recovered vapor product.

[0025] The condensation of a portion of the product into vapor, as described above, provides a particularly effective removal of impurities from the vapor product. In particular, high-boiling-point components, for example, having a boiling point > 410°C, Petition 870260022828, dated 12 / 03 / 2026, page 18 / 65 10 / 18 can thus be effectively removed. This is especially advantageous in the case of hydrocarbon mixtures obtained from the depolymerization of plastic materials, particularly plastic waste, since these materials often comprise undesirable organophosphorus compounds, for example, the compound tris(2,4-di-tert-butylphenyl) phosphite. These compounds can be at least partially removed from the vapor product by condensing a portion of the vapor product exiting the inner volume of the outer container through the top outlet, and transporting the condensed portion of the vapor product back to the inner volume of the outer container.

[0026] The vapor product, recovered from the inventive process, can be fed to other downstream separation and / or washing stages. Preferably, it can be fed to a downstream separation column for separation of the vapor product into different product streams by distillation.

[0027] With regard to the inventive apparatus, it is preferred if the internal volume of the outer container, in the first section, has a substantially elliptical cross-section, preferably a substantially circular cross-section. It is especially preferred if the internal volume of the outer container, in the first section, is substantially cylindrical or substantially truncated conical, preferably substantially cylindrical. Similarly, it is preferred if the internal volume of the outer container, in the second section, has a substantially elliptical cross-section, preferably a substantially circular cross-section. It is especially preferred if the internal volume of the outer container, in the second section, is substantially cylindrical or substantially truncated conical, preferably substantially cylindrical.With regard to all embodiments of the invention, it is preferred that both the internal volume of the outer container, in the first section, and the internal volume of the outer container, in the second section, be... Petition 870260022828, dated 12 / 03 / 2026, page 19 / 65 11 / 18 substantially cylindrical or substantially truncated conical, especially substantially cylindrical.

[0028] In a preferred embodiment of the inventive apparatus, the first section comprises a second tangential inlet, arranged to introduce a stream of multiphase hydrocarbons tangentially into the internal volume of the outer vessel to create a vortex flow. By providing a second tangential inlet, it is possible to distribute the introduction of the hydrocarbon stream through two separate inlets. This allows increasing the total amount of material entering the internal volume of the outer vessel, while maintaining the flow velocity at the tangential inlet sufficiently low to reduce erosion caused by the solids contained in the multiphase hydrocarbon stream. Furthermore, the second tangential inlet can serve as an alternative in case the first tangential inlet becomes clogged.

[0029] In another preferred embodiment of the inventive apparatus, the second section comprises a lower tangential inlet, arranged to introduce a stream tangentially into the internal volume of the outer container. The lower tangential inlet can be used to further increase the tangential velocity of the vortex flow in the second section. This reduces the residence time and thus the tendency to coking, while simultaneously promoting greater centrifugal force and thus better separation in that section. In a preferred embodiment of the inventive process, at least a portion of the recovered solids-enriched product stream is recycled and introduced through the lower tangential inlet into the second section of the internal volume of the outer container, preferably to further increase the tangential velocity of the vortex flow.

[0030] In a preferred embodiment, the body of the inner container is substantially cylindrical or substantially frustum-conical, of Petition 870260022828, dated 12 / 03 / 2026, page 20 / 65 12 / 18 preferably, substantially cylindrical. Preferably, the longitudinal axis of the inner container body is arranged substantially coaxially with the longitudinal axis of the outer container body. Preferably, at least a portion of the inner container body is arranged within the second section of the outer container body.

[0031] Preferably, the internal volume of the inner container has a ratio of its length along the longitudinal axis to the diameter of its cross-sectional area between 0.5 and 10, particularly between 1 and 6, more particularly between 1.6 and 4, especially between 2.2 and 3.0. In this regard, it is especially preferred if the internal volume of the outer container is substantially cylindrical.

[0032] In a preferred embodiment, the inner vessel comprises an internal top outlet, oriented towards the top end of the outer vessel and in fluid communication with the internal volume of the outer vessel and the internal volume of the inner vessel. This top outlet allows vapor to exit the internal volume of the inner vessel and be transported to the top outlet. Preferably, the through conduit passes through the body of the outer vessel at a position that is even further down the longitudinal axis than the internal top outlet of the inner vessel, so that the liquid stream exits the inner vessel through the through conduit before the inner vessel overflows.

[0033] In this regard, it is preferred if the inner container comprises a barrier, disposed between the inner top outlet and the top end of the outer container, wherein said barrier is disposed to, at least partially, prevent the entry of solids into the inner volume of the inner container through the inner top outlet, but allow fluids, for example, steam, to exit the inner volume of the inner container through the inner top outlet. Preferably, said barrier is conical, having an apex oriented towards the top end of the Petition 870260022828, dated 12 / 03 / 2026, page 21 / 65 13 / 18 outer container.

[0034] In a preferred embodiment of the inventive process, the apparatus is operated at a temperature between 320°C and 450°C, preferably between 360°C and 400°C. Preferably, the temperature of the multiphase hydrocarbon stream at the tangential inlet is between 300°C and 480°C, particularly between 330°C and 450°C, more particularly between 350°C and 420°C, especially between 360°C and 400°C.

[0035] Preferably, the multiphase hydrocarbon stream is obtained from a hydrocarbon cracking reactor, which is preferably fluid-connected to the tangential inlet via a tangential conduit. In a preferred embodiment, the solids-enriched product stream recovered by the through conduit is recycled to said hydrocarbon cracking reactor.

[0036] With regard to the invention, it is preferred that the multiphase hydrocarbon stream be obtained from the depolymerization of plastic materials, preferably plastic waste, especially pre-consumer, post-consumer and / or post-industrial plastics. Preferably, the plastic materials comprise polyolefins, preferably selected from polyethylene and polypropylene, and / or polystyrene. The depolymerization of plastics may preferably be by pyrolysis, especially by non-catalytic thermal cracking or by catalytic cracking.

[0037] In a preferred embodiment, the multiphase hydrocarbon stream comprises selected impurities of aluminum powder and / or organophosphorus compounds, especially tris(2-4-di-tert-butylphenyl) phosphite. These impurities are commonly present in plastic materials, especially plastic waste. As described in this descriptive report, the inventive apparatus is particularly well suited for effectively removing at least part of these impurities.

[0038] The present invention is further illustrated by the figures Petition 870260022828, dated 12 / 03 / 2026, page 22 / 65 14 / 18 presented below, but not limited to them.

[0039] Figure 1 shows a longitudinal section of a preferred embodiment of the apparatus according to the invention.

[0040] Figure 2 shows a processing flowchart for a facility for processing plastic waste, comprising a preferred embodiment of the apparatus according to the invention.

[0041] The apparatus, shown in Figure 1, comprises an outer container 1 having a top end 2 comprising a top outlet 3, a bottom end 4 comprising a bottom outlet 5, with a longitudinal axis 6 extending between the top end 2 and the bottom end 4. The outer container 1 further comprises an outer container body 7, disposed between the top end 2 and the bottom end 4 and having an inner volume of the outer container 8 in fluid communication with the top outlet 3 and the bottom outlet 5. The outer container body 7 comprises a first section 9 comprising a tangential inlet 10, and a second section 11, disposed closer to the bottom end 4 than the first section 9. In the illustrated embodiment, both the first section 9 and the second section 11 are substantially cylindrical. They are connected to each other by a third substantially truncated conical section 12 of the outer container body 7.The tangential inlet 10 is arranged to introduce the multiphase hydrocarbon stream 27 tangentially into the internal volume of the outer vessel 8 to create a vortex flow. This can be achieved by injecting the stream tangentially onto the internal surface of the outer vessel body 7 to create a vortex flow on said internal surface, in a manner similar to that commonly done in cyclone separators. Furthermore, in the illustrated embodiment, the first section 9 comprises a second tangential inlet 13, which may be similar, in some respects, to the tangential inlet 10. The internal volume of the vessel. Petition 870260022828, dated 12 / 03 / 2026, page 23 / 65 15 / 18 external 8 has a smaller cross-sectional circumference in the second section 11 than in the first section 9, which, during operation, provides a higher tangential velocity of the vortex flow in the second section 11 than in the first section 9. In the illustrated embodiment, the second section 11 comprises a lower tangential inlet 14, which can be used to introduce a liquid stream to further increase the tangential velocity of the vortex flow in the second section 11.

[0042] The apparatus, shown in Figure 1, further comprises an inner container 15, disposed within the body of the outer container 7. The inner container 15 comprises a body of the inner container 16, having an inner container volume 17 and an inner bottom inlet 18, oriented towards the bottom end 4 of the outer container 1 and providing fluid connection of the inner volume of the inner container 17 with the inner volume of the outer container 8. In addition, in the illustrated configuration, the inner container 15 comprises an inner top outlet 19, oriented towards the top end 2 of the outer container 1 and providing fluid connection of the inner volume of the inner container 17 with the inner volume of the outer container 8.A barrier 20 is disposed between the inner top outlet 19 and the top end 2 to prevent, at least partially, the entry of solids into the internal volume of the inner container 17, while allowing fluids, such as vapors, to exit through the inner top outlet 19, for example, to be transported to the top outlet 3. The apparatus further comprises a through conduit 21, in fluid communication with the internal volume of the inner container 17, which through conduit 21 passes through the body of the outer container 7, so that a product stream can be transported from the internal volume of the inner container 17 to the outside of the outer container.

[0043] For operation of the device, shown in Figure 1, in Petition 870260022828, dated 12 / 03 / 2026, page 24 / 65 16 / 18 Inventive process, a multi-phase hydrocarbon stream 27, obtained, for example, from the depolymerization of plastic material in a cracking reactor 26, as shown in Figure 2, can be introduced into the internal volume of the outer vessel 8 through the tangential inlet 10 and / or the second tangential inlet 13 to create a vortex flow. As a consequence of centrifugal force, solids and liquids are pushed towards the inner surface of the outer vessel body 7, while the vaporous components are separated by radial movement inwards and transported to the top outlet 3. Preferably, the circumference in cross-section, in the first section 9, is low enough to ensure that the axial velocity of the vapor product 30, which moves towards the top outlet 3, is low enough to reduce the entrainment of liquid droplets.The vapor product 30, exiting the internal volume of the external container 8, can be partially condensed in a cooling system, for example, by spraying a fluid onto the vapor product 30 using one or more spray nozzles 33. Said fluid can be obtained by condensing and recycling a portion of the recovered vapor product 30. The condensation step allows for the condensation, preferably, of impurities having a boiling point higher than that of the desirable components of the vapor product 30, for example, undesirable organophosphorus compounds commonly found in plastic materials. The condensed portion of the vapor product 30 is transferred back to the internal volume of the external container 8 and can be, at least partially, removed by the reduced-solids product stream 25 and / or by the solids-enriched product stream 28.

[0044] After product separation into vapor 30, the remaining hydrocarbon stream is transported from the first section 9, through the third section 12, to the second section 11, whereby the tangential velocity of the vortex flow is increased due to the circumference at. Petition 870260022828, dated 12 / 03 / 2026, page 25 / 65 17 / 18 decreasing cross-section. The higher tangential velocity results in a shorter residence time, thus reducing the tendency to coking. At the same time, the higher tangential velocity generates a greater centrifugal force, and therefore a more effective separation. Through this centrifugal force, the hydrocarbon stream is separated into a solids-enriched product stream 28 and a reduced-solids product stream 25. The solids-enriched product stream 28 is transported to the bottom outlet. The reduced-solids product stream 25 generates liquid retention in the internal volume of the outer vessel 8 and thus enters the internal volume of the inner vessel 17 through the internal bottom inlet 18, eventually reaching the through conduit 21, from which it can be recovered.Advantageously, the reduced solids product stream enters the through conduit 21 at an inlet opening 21a and exits the through conduit 21 at an outlet opening 21b, wherein the outlet opening 21b is disposed outside the body of the outer container 7 and below the inlet opening 21a. Preferably, the through conduit 21 passes through the body of the outer container 7 to a position that is further down along the longitudinal axis 6 than the inner top outlet 19 of the inner container 15.

[0045] Advantageously, the recovered solids-enriched product stream 25 can be recycled back to the cracking reactor 26 for further cracking. The solids-enriched product stream 28 is recovered from the bottom outlet and can be fed to other downstream separation stages, for example, to a coke collector 29. A portion of the solids-enriched product stream 28 can be recycled and introduced into the lower tangential inlet 14 to further increase the tangential velocity of the vortex flow in the second section 11.

[0046] An application of a preferred mode of the device Petition 870260022828, dated 12 / 03 / 2026, page 26 / 65 The inventive apparatus, in a plastics processing plant, can be seen in Figure 2. The plastic material is fed to an extruder 23, where it is compacted, melted and / or degassed. The molten plastic material, preferably at a temperature between 250°C and 280°C, is mixed in a static mixer 22 with an external solvent 24, preferably heavy oil, and / or at least part of the reduced solids product stream 25 obtained from the inventive apparatus, to reduce the viscosity of the liquid plastic bath. The resulting mixture is then conveyed to a cracking reactor 26, where the plastic is depolymerized at a temperature between 400°C and 440°C. From the cracking reactor 26, a multi-phase hydrocarbon stream 27 is obtained, which is then introduced into the outer vessel 1 of the inventive apparatus through the tangential inlet 10, as described above in this descriptive report.At least a portion of the reduced-solids product stream 25, obtained from the inventive apparatus, can be recycled and fed to a fresh plastic liquid bath, preferably together with solvent 24. The solids-enriched product stream 28 is conveyed to a coke collector 29 to remove coke particles, and at least a portion of the resulting stream can be recycled and injected into the lower tangential inlet 14 of the inventive apparatus, as described above. The vapor product 30, obtained from the inventive apparatus, is further separated into a light product 31, preferably having a boiling point range of 35°C to 225°C, and a heavy product 32, preferably having a boiling point range of 225°C to 410°C. A portion of the heavy product 32 can be recycled to a spray nozzle 33, arranged to cool and condense a portion of the product into vapor 30, as described above in this descriptive report. Petition 870260022828, dated 12 / 03 / 2026, p. 27 / 65

Claims

1 / 5 CLAIMS 1. Apparatus for separating the components of a multi-phase hydrocarbon stream (27), characterized in that it comprises: - an outer container (1) having a top end (2), comprising a top outlet (3), a bottom end (4), comprising a bottom outlet (5), with a longitudinal axis (6) extending between the top end (2) and the bottom end (4), and an outer container body (7), disposed between the top end (2) and the bottom end (4) and having an inner volume of the outer container (8), in fluid communication with the top outlet (3) and the bottom outlet (5), wherein the outer container body (7) comprises: - a first section (9), comprising a tangential inlet (10), disposed to introduce the multi-phase hydrocarbon stream (27) tangentially into the inner volume of the outer container (8) to create a vortex flow;and - a second section (11) disposed closer to the bottom end (4) than the first section (9), wherein the internal volume of the outer container (8) has a smaller cross-sectional circumference in the second section (11) than in the first section (9); - an inner container (15) disposed within the body of the outer container (7), said inner container (15) comprising: - a body of the inner container (16) having an internal volume of the inner container (17); - an internal bottom inlet (18) oriented towards the bottom end (4) of the outer container (1) and in fluid communication with the internal volume of the inner container (17) and with the internal volume of the outer container (8); - an internal top outlet (19) oriented towards Petition 870260022828, dated 12 / 03 / 2026, page. 28 / 65 2 / 5 top end (2) of the outer container (1) and in fluid communication with the inner volume of the outer container (8) and with the inner volume of the inner container (17);and - a through conduit (21) in fluid communication with the internal volume of the inner container (17) and passing through the body of the outer container (7), so that a product stream can be transported from the internal volume of the inner container (17) out of the outer container (1), wherein the through conduit (21) passes through the body of the outer container (7), at a position that is even lower along the longitudinal axis (6) than the internal top outlet (19) of the inner container (15).; 2. Apparatus, according to claim 1, characterized in that the ratio of the circumference in cross-section of the internal volume of the external container (8), in the second section (11), to the circumference in cross-section of the internal volume of the external container (8), in the first section (9), is between 0.05 and 0.95, preferably between 0.1 and 0.9, more preferably between 0.25 and 0.8, even more preferably between 0.4 and 0.7, most preferably between 0.5 and 0.

6.

3. Apparatus, according to claim 1 or 2, characterized in that it further comprises a cooling system, fluid-connected to the top outlet (3), wherein the cooling system is adapted to condense a portion of a product into vapor (30), which exits the internal volume of the outer container (8) through the top outlet (3), and transport the condensed portion of the product into vapor (30) back to the internal volume of the outer container (8), preferably wherein the cooling system comprises at least one spray nozzle (33).

4. Apparatus, according to any one of claims 1 to 3, characterized in that the internal volume of the external container (8), in the first section (9) and / or in the second section (11), is Petition 870260022828, dated 12 / 03 / 2026, page 29 / 65 3 / 5 substantially cylindrical or substantially truncated conical, preferably substantially cylindrical.

5. Apparatus, according to any one of claims 1 to 4, characterized in that the first section (9) comprises a second tangential inlet (13), arranged to introduce the multiphase hydrocarbon stream (27) tangentially into the internal volume of the outer container (8) to create a vortex flow.

6. Apparatus, according to any one of claims 1 to 5, characterized in that the second section (11) comprises a lower tangential inlet (14), arranged to introduce a stream tangentially into the internal volume of the outer container (8).

7. Apparatus, according to any one of claims 1 to 6, characterized in that the inner container (15) comprises a barrier (20), disposed between the inner top outlet (19) and the top end (2) of the outer container (1), wherein said barrier (20) is disposed to prevent, at least partially, the entry of solids into the inner volume of the inner container (17) through the inner top outlet (19), but to allow fluids to exit the inner volume of the inner container (17) through the inner top outlet (19).

8. Process for separating components of a multi-phase hydrocarbon stream (27) in an apparatus, as defined in any one of claims 1 to 7, characterized in that it comprises the steps of: - introducing the multi-phase hydrocarbon stream (27), through the tangential inlet (10), into the internal volume of the external container (8) to create a vortex flow, whereby a vapor product (30) is separated from the hydrocarbon stream and transported to the top outlet (3); - recovering said vapor product (30) from the top outlet (3); Petition 870260022828, dated 12 / 03 / 2026, p.30 / 65 4 / 5 - transport the hydrocarbon stream from the first section (9) to the second section (11), thereby increasing the tangential velocity of the vortex flow, wherein the hydrocarbon stream is separated into a solids-enriched product stream (28) and a reduced-solids product stream (25), wherein the solids-enriched product stream (28) is transported to the bottom outlet (5); - recover the solids-enriched product stream (28) from the bottom outlet (5); - transport the reduced-solids product stream (25) to the internal volume of the inner vessel (17) through the bottom inlet of the inner vessel (18); and - recover the reduced-solids product stream (25) from the internal volume of the inner vessel (17) through the through conduit (21).

9. Process, according to claim 8, characterized in that it further comprises the step of condensing a portion of the product into vapor (30), which exits the internal volume of the outer container (8) through the top outlet (3), and transporting the condensed portion of the product into vapor (30), back to the internal volume of the outer container (8).

10. Process, according to claim 9, characterized in that said condensation is carried out by spraying a fluid onto the vapor product (30), wherein the temperature of said fluid is lower than the temperature of the vapor product (30), preferably wherein the temperature of the fluid is between 120°C and 350°C, preferably between 150°C and 300°C, especially between 180°C and 250°C.

11. Process, according to claim 10, characterized in that said fluid is obtained by condensation and recycling of a portion of the product in recovered vapor (30). Petition 870260022828, dated 12 / 03 / 2026, page 31 / 65 5 / 5 12. Process, according to any one of claims 8 to 11, characterized in that the temperature of the multiphase hydrocarbon stream (27), at the tangential inlet (10), is between 300°C and 480°C, preferably between 330°C and 450°C, more preferably between 350°C and 420°C, especially between 360°C and 400°C.

13. Process, according to any one of claims 8 to 12, characterized in that the multiphase hydrocarbon stream (27) is obtained from the depolymerization of plastic materials, preferably plastic waste.

14. Process according to claim 13, characterized in that the plastic materials comprise polyolefins, preferably selected from polyethylene and polypropylene, and / or polystyrene.

15. Process, according to any one of claims 8 to 14, characterized in that the multi-phase hydrocarbon stream (27) comprises selected impurities of aluminum powder and / or organophosphorus compounds, especially tris(2,4-di-tert-butylphenyl)phosphite. Petition 870260022828, dated 12 / 03 / 2026, p. 32 / 65

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