Apparatus and process for separating components of a multiphase hydrocarbon stream

Abstract

The present invention relates to an apparatus and process for separating components of a multiphase hydrocarbon stream (27), said apparatus comprising: - an outer container (1) having an upper end (2) with an upper outlet (3), a lower end (4) with a lower outlet (5), and an outer container body (7) disposed between the upper end (2) and the lower end (4) and having an outer container interior space (8) in fluid communication with the upper outlet (3) and the lower outlet (5), the outer container having a longitudinal axis (6) extending between the upper end (2) and the lower end (4); The outer container body (7) is - a first section (9) with a tangential inlet (10) arranged to introduce a multiphase hydrocarbon stream (27) tangentially into the outer vessel volume (8) to create a vortex flow; and - a second section (11) disposed closer to the lower end (4) than the first section (9), and the outer container space (8) has a smaller cross-sectional perimeter in the second section (11) than in the first section (9); An outer container (1), - an inner container (15) arranged within the outer container body (7), the inner container (15) comprising: - an inner container body (16) having an inner container space (17); and - an inner lower inlet (18) facing towards the lower end (4) of the outer vessel (1) and in fluid communication with the inner vessel space (17) and with the outer vessel space (8); An inner container (15) comprising: - a traverse conduit (21) in fluid communication with the inner vessel space (17) and traversing the outer vessel body (7); Equipped with.

Description

[Technical Field]

[0001] The present invention relates to an apparatus and process for separating components of a multiphase hydrocarbon stream. [Background technology]

[0002] Hydrocarbon cracking processes generally involve the decomposition of long-chain hydrocarbons into shorter-chain hydrocarbons at moderate or high temperatures, for example 400-600° C. (thermal cracking) and / or in the presence of a catalyst (catalytic cracking). A particularly interesting application of cracking processes is the depolymerization of plastic materials, which are used for the recycling of plastic waste.

[0003] Cracking processes typically produce complex mixtures of hydrocarbons that must be at least partially separated. Such mixtures obtained from cracking reactors are typically multiphase systems containing vapor, liquid, and possibly solid components. For example, the vapor phase may contain the desired cracked hydrocarbons, the liquid phase may contain hydrocarbons that have not yet been fully cracked, and the solid phase may contain coke particles. In addition, impurities may also be present, particularly in the context of recycling plastic waste. In addition to coke particles, solid impurities may include, for example, aluminum powder, fillers, or ash. Vapor impurities may include, for example, certain organophosphorus components commonly used in plastic materials.

[0004] WO 2020 / 168062(A1) discloses a process for removing coke and tar from a steam cracking furnace effluent, in which the quenched furnace effluent is introduced into a centrifuge, where a vapor product is separated from a centrifuge sediment containing at least a portion of the coke and / or tar.

[0005] U.S. Pat. No. 2,776,931 discloses a process and apparatus for quenching and separating hot exhaust vapors from a coking operation in which the hot exhaust vapors are quenched, thereby liquefying certain high-boiling contaminants, and then in a cyclone separation zone, liquids and solids are separated from the remaining quenched vapors.

[0006] U.S. Pat. No. 2,927,890 discloses a process involving the separation and quenching of gaseous products from the thermal conversion of a residual petroleum feed, the quench stream being passed through a cyclone separation zone to separate uncondensed vapors from entrained solids and liquid streams, and then the liquid stream being separated from the solids. Summary of the Invention [Problem to be solved by the invention]

[0007] It is an object of the present invention to at least alleviate one or more of the disadvantages of the prior art. In particular, it is an object of the present invention to provide an apparatus and process that allows for at least partial separation of the vapor, liquid, and solid components of a multiphase hydrocarbon stream in a single facility. Additionally, it is a further object of the present invention to provide an apparatus and process that allows for more efficient removal of impurities from multiphase hydrocarbon streams, in particular from multiphase hydrocarbon streams obtained from the depolymerization of plastic materials. [Means for solving the problem]

[0008] To this end, the present invention provides an apparatus for separating components of a multiphase hydrocarbon stream, said apparatus comprising: an outer vessel having an upper end with an upper outlet, a lower end with a lower outlet, and an outer vessel internal volume disposed between said upper end and said lower end and in fluid communication with said upper outlet and said lower outlet, said outer vessel having a longitudinal axis extending between said upper end and said lower end; The outer container body is a first section including a tangential inlet arranged to introduce the multiphase hydrocarbon stream tangentially into the outer vessel volume to create a vortex flow; and a second section disposed closer to the lower end than the first section, wherein the outer container space has a smaller cross-sectional perimeter in the second section than in the first section; an outer container comprising: an inner container disposed within the outer container, the inner container comprising: an inner vessel body having an inner vessel internal volume; and an inner lower inlet facing the lower end of the outer container and in fluid communication with the inner container space and the outer container space; an inner container comprising: - a traversing conduit in fluid communication with the inner vessel space and traversing the outer vessel body; Equipped with.

[0009] In another aspect, the present invention provides a process for separating components of a multiphase hydrocarbon stream in an apparatus according to the present invention, said process comprising: - introducing the multiphase hydrocarbon stream into the outer vessel volume through the tangential inlet to create a vortex flow whereby vapor products are separated from the hydrocarbon stream and conveyed to the top outlet; - recovering the vapor product from the top outlet; - conveying the hydrocarbon stream from the first section to the second section, thereby increasing the tangential velocity of the vortex flow, wherein the hydrocarbon stream is separated into a solids-enriched product stream and a solids-depleted product stream, and the solids-enriched product stream is conveyed to the bottom outlet; - recovering the solids-enriched product stream from the bottom outlet; - conveying the solids-reduced product stream through the inner vessel lower inlet into the inner vessel interior space; and - recovering the solids-reduced product stream from the inner vessel volume through the traverse conduit; Includes.

[0010] The apparatus and process of the present invention allow for at least partial separation of the vapor, liquid, and solid components of a multiphase hydrocarbon stream in a single facility. In the context of the present invention, the term "multiphase" means the presence of two or more phases of matter. Preferably, the multiphase hydrocarbon stream comprises at least three phases, in particular a vapor, liquid, and solid component. The first section of the apparatus of the present invention advantageously allows for the separation of vapor from liquids and solids, and the second section advantageously allows for the separation of the liquid / solid mixture into a solids-enriched product stream and a solids-depleted product stream. Performing these two separation processes in a single facility reduces costs and complexity while simultaneously increasing efficiency. In addition, piping and control valves that would otherwise be required to connect separate separation devices can be avoided, leading to increased robustness and a reduced failure rate due to, for example, blockages.

[0011] In the apparatus of the present invention, the outer vessel space has a smaller cross-sectional perimeter in the second section of the outer vessel body than in the first section. Unless otherwise specified, as used herein, the term "cross-section" refers to a section intersecting a plane substantially perpendicular to the longitudinal axis. Accordingly, the cross-sectional perimeter of the outer vessel space refers to the perimeter of the region of the outer vessel space in a cross-sectional plane substantially perpendicular to the longitudinal axis of the outer vessel. The first section of the outer vessel body enables separation of vapor from liquid and solids according to the principle of cyclone separation. Solid and liquid components are pushed radially outward toward the inner surface of the outer vessel body by centrifugal force and continue to move axially toward the second section, while vapor components are pushed radially inward and move axially upward toward the upper outlet. Providing a larger cross-sectional perimeter in the first section reduces the axial velocity of the vapor product moving toward the top outlet, which advantageously reduces entrainment of liquid droplets with the vapor and therefore improves separation effectiveness. At the same time, providing a smaller cross-sectional perimeter in the second section increases the tangential velocity of the vortex flow in the second section, which advantageously reduces residence time and thereby reduces coking tendency. At the same time, the higher tangential velocity in the second section leads to higher centrifugal forces, thereby improving separation efficiency in this section.

[0012] Preferably, the ratio of the cross-sectional perimeter of the space within the outer container in the second section to the cross-sectional perimeter of the space within the outer container in the first section is less than 0.95, preferably less than 0.9, more preferably less than 0.8, even more preferably less than 0.7, and most preferably less than 0.6. It is particularly preferred if the ratio 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, and most preferably between 0.5 and 0.6.

[0013] Preferably, the ratio of the outer container space of the first section to its extension along the longitudinal axis to its cross-sectional area diameter is between 0.2 and 5, preferably between 0.33 and 3, more preferably between 0.5 and 2, even more preferably between 0.75 and 1.8, and most preferably between 1 and 1.4. In this context, it is particularly preferred if the outer container space of the first section is substantially cylindrical.

[0014] Preferably, the ratio of the outer container space of the second section to its extension along the longitudinal axis to its cross-sectional area diameter is between 0.4 and 10, preferably between 0.66 and 6, more preferably between 1 and 4, even more preferably between 1.33 and 3, and most preferably between 1.6 and 2.5. In this context, it is particularly preferred if the outer container space of the second section is substantially cylindrical.

[0015] In a preferred embodiment, the device further comprises a third section connecting the first section and the second section, and the space within the outer container of the third section is preferably substantially frustoconical.

[0016] In a preferred embodiment of the process of the present invention, the tangential velocity of said vortex flow in said first section is 0.01-20 m / s, preferably 0.05-10 m / s, more preferably 0.1-5 m / s, most preferably 0.2-2.5 m / s.

[0017] It is further preferred if the tangential velocity of said vortex flow in said second section is 0.05-10 m / s, preferably 0.1-5 m / s, more preferably 0.25-2.5 m / s, most preferably 0.5-2 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 0.05 to 0.99, preferably 0.1 to 0.95, more preferably 0.2 to 0.9, even more preferably 0.3 to 0.8, and most preferably 0.4 to 0.7.

[0019] In a further preferred embodiment, the mean residence time of the vortex flow in the second section is 0.1 to 30 minutes, preferably 0.2 to 10 minutes, more preferably 0.5 to 8 minutes, and most preferably 0.8 to 6 minutes. Preferably, the mean residence time is determined by CFD simulation.

[0020] The tangential inlet provided in the first section of the outer vessel body is arranged so as to create a vortex flow within the outer vessel space when the multiphase hydrocarbon stream is introduced through the tangential inlet. Such an arrangement is well known to those skilled in the art as it is commonly used in cyclone separators. Preferably, the tangential inlet is arranged tangentially with respect to a cross-sectional area of ​​the outer vessel space in a plane substantially perpendicular to the longitudinal axis.

[0021] In a preferred embodiment, the apparatus further comprises a tangential conduit in fluid communication with the tangential inlet, preferably the tangential conduit comprising a flash valve. Preferably, the tangential conduit is fluidly connected to a hydrocarbon cracking reactor. The provision of a flash valve enables flash vaporization of the hydrocarbon stream, where the hydrocarbon stream is subjected to a pressure reduction and at least some of the components of the hydrocarbon stream are transferred from a liquid phase to a vapor phase.

[0022] In the context of the apparatus of the present invention, it is preferred if the ratio of the cross-sectional perimeter of the inner vessel space to the cross-sectional perimeter of the outer vessel space in the second section is at least 0.1, preferably at least 0.25, more preferably at least 0.4, even more preferably at least 0.5, and even more preferably at least 0.6. It is particularly preferred if the ratio is between 0.1 and 0.99, preferably between 0.25 and 0.95, more preferably between 0.4 and 0.9, even more preferably between 0.5 and 0.85, and even more preferably between 0.6 and 0.8. A high ratio has the advantage that a greater proportion of the outer vessel space is occupied by the inner vessel body, which leads to an increase in the tangential velocity of the vortex flow. This advantageously reduces the residence time and thus the tendency to coke, while at the same time providing higher centrifugal forces, which can improve separation.

[0023] Preferably, the solids-enriched product stream has a higher solids content than the solids-depleted product stream, preferably at least 5%, more preferably at least 10%, even more preferably at least 20%, and even more preferably at least 50% higher. Preferably, as used herein, the solids content corresponds to the ash content. The ash content is preferably determined in accordance with ISO 6245:2001.

[0024] In a preferred embodiment, the apparatus of the present invention further comprises a cooling system fluidly connected to the upper outlet, the cooling system configured to condense a portion of the vapor product discharged from the outer vessel interior space through the upper outlet and convey the condensed portion of the vapor product back to the outer vessel interior space. Preferably, the cooling system comprises at least one spray nozzle. Similarly, in a preferred embodiment of the process of the present invention, the process further comprises the step of condensing a portion of the vapor product discharged from the outer vessel interior space through the upper outlet and conveying the condensed portion of the vapor product back to the outer vessel interior space. Preferably, the condensation is achieved by spraying a fluid onto the vapor product, the fluid having a temperature lower than that of the vapor product. Preferably, the fluid has a temperature of 120°C to 350°C, preferably 150°C to 300°C, particularly 180°C to 250°C. It is further preferred if the fluid is obtained by condensing and recycling a portion of the recovered vapor product.

[0025] Condensing a portion of the vapor product as described above allows for particularly effective removal of impurities from the vapor product. In particular, high-boiling components, e.g., components having a boiling point above 410°C, can be effectively removed by this method. This is particularly advantageous in the case of hydrocarbon mixtures obtained from the depolymerization of plastic materials, particularly plastic waste, because such materials often contain undesirable organophosphorus compounds, such as tris(2,4-di-tert-butylphenyl)phosphite. Such compounds can be at least partially removed from the vapor product by condensing a portion of the vapor product discharged from the outer vessel space through the upper outlet and transporting the condensed portion of the vapor product back into the outer vessel space.

[0026] The vapor product recovered from the process of the present invention may be fed to further downstream separation and / or washing steps, preferably to a downstream separation column for separating the vapor product into different product streams by distillation.

[0027] In the context of the device of the present invention, it is preferred that the space within the outer container in the first section has a substantially elliptical cross section, preferably a substantially circular cross section. It is particularly preferred that the space within the outer container in the first section is substantially cylindrical or substantially frusto-conical, preferably substantially cylindrical. Similarly, it is preferred that the space within the outer container in the second section has a substantially elliptical cross section, preferably a substantially circular cross section. It is particularly preferred that the space within the outer container in the second section is substantially cylindrical or substantially frusto-conical, preferably substantially cylindrical. In relation to all aspects of the present invention, it is preferred that both the space within the outer container in the first section and the space within the outer container in the second section are substantially cylindrical or substantially frusto-conical, in particular substantially cylindrical.

[0028] In a preferred embodiment of the apparatus of the present invention, the first section includes a second tangential inlet positioned to introduce the multiphase hydrocarbon stream tangentially into the outer vessel space to create a vortex. The provision of the second tangential inlet allows the introduction of the hydrocarbon stream to be distributed between two separate inlets. This allows the total amount of material entering the outer vessel space to be increased while maintaining the flow velocity at the tangential inlet low enough to reduce erosion caused by solids contained in the multiphase hydrocarbon stream. In addition, the second tangential inlet may serve as a backup in case the first tangential inlet becomes blocked.

[0029] In another preferred embodiment of the apparatus of the present invention, the second section comprises a lower tangential inlet arranged to introduce a flow tangentially into the outer vessel space. The lower tangential inlet can be used to further increase the tangential velocity of the vortex flow in the second section. This allows for a shorter residence time and therefore a reduced tendency to coke, while also providing higher centrifugal forces to improve separation in this section. In a preferred embodiment of the process of the present invention, at least a portion of the recovered solids-enriched product stream is preferably recycled and introduced into the second section of the outer vessel space through the lower tangential inlet to further increase the tangential velocity of the vortex flow.

[0030] In a preferred embodiment, the inner container body is substantially cylindrical or substantially frustoconical, preferably substantially cylindrical. Preferably, the longitudinal axis of the inner container body is substantially coaxial with the longitudinal axis of the outer container body. Preferably, at least a portion of the inner container body is located within the second section of the outer container body.

[0031] Preferably, the ratio of the inner container space's extent along the longitudinal axis to its cross-sectional area diameter is between 0.5 and 10, more preferably between 1 and 6, even more preferably between 1.6 and 4, and most preferably between 2.2 and 3.0. In this context, it is particularly preferred that the inner container space is substantially cylindrical.

[0032] In a preferred embodiment, the inner vessel includes an internal upper outlet facing the upper end of the outer vessel and in fluid communication with the outer vessel interior space and the inner vessel interior space. Such an upper outlet allows vapor to be discharged from the inner vessel interior space and conveyed to the upper outlet. Preferably, the traverse conduit traverses the outer vessel body at a position further below the internal upper outlet of the inner vessel along the longitudinal axis so that liquid flow is discharged from the inner vessel through the traverse conduit before the inner vessel overflows.

[0033] In this context, it is preferred if the inner container comprises a barrier arranged between the inner upper outlet and the upper end of the outer container, the barrier being arranged to at least partially block solids from entering the inner container space through the inner upper outlet but to allow fluids, for example steam, to exit the inner container space through the inner upper outlet. Preferably, the barrier is conical, with an apex pointing towards the upper end of the outer container.

[0034] In a preferred embodiment of the process of the present invention, the apparatus is operated at a temperature of from 320° C. to 450° C., preferably from 360° C. to 400° C. Preferably, the temperature of the multiphase hydrocarbon stream at the tangential inlet is from 300° C. to 480° C., preferably from 330° C. to 450° C., more preferably from 350° C. to 420° C., most preferably from 360° C. to 400° C.

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

[0036] In the context of the present invention, it is preferred that the multiphase hydrocarbon stream is obtained from the depolymerization of plastic material, preferably plastic waste, in particular pre-consumer, post-consumer and / or post-industrial plastics. Preferably, the plastic material comprises a polyolefin, preferably selected from polyethylene and polypropylene, and / or polystyrene. The depolymerization of plastics may preferably be by pyrolysis, in particular uncatalyzed pyrolysis, or by catalytic decomposition.

[0037] In a preferred embodiment, the multiphase hydrocarbon stream contains impurities selected from aluminum powder and / or organophosphorus compounds, particularly tris(2,4-di-tert-butylphenyl) phosphite. Such impurities are commonly present in plastic materials, particularly plastic waste. As described herein, the apparatus of the present invention is particularly well suited for effectively removing at least a portion of such impurities.

[0038] The present invention is further illustrated by, but not limited to, the following figures. [Brief explanation of the drawings]

[0039] [Figure 1] FIG. 1 shows a longitudinal section of a preferred embodiment of the device according to the invention. [Figure 2] FIG. 2 shows a process flow diagram for a plastic waste treatment facility including a preferred embodiment of an apparatus according to the present invention. DETAILED DESCRIPTION OF THE INVENTION

[0040] The apparatus shown in FIG. 1 includes an outer vessel 1 having an upper end 2 with an upper outlet 3 and a lower end 4 with a lower outlet 5, with a longitudinal axis 6 extending between the upper end 2 and the lower end 4. The outer vessel 1 further includes an outer vessel body 7 disposed between the upper end 2 and the lower end 4 and having an outer vessel interior space 8 in fluid communication with the upper and lower outlets 3 and 5. The outer vessel body 7 includes a first section 9 with a tangential inlet 10 and a second section 11 disposed closer to the lower end 4 than the first section 9. In the illustrated embodiment, the first and second sections 9 and 11 are both substantially cylindrical. They are connected by a substantially frusto-conical third section 12 of the outer vessel body 7. The tangential inlet 10 is positioned to introduce a multiphase hydrocarbon stream 27 tangentially into the outer vessel interior space 8 to create a vortex flow. This can be achieved by injecting the stream tangentially against the inner surface of the outer vessel body 7 to create a vortex flow on the inner surface, as is commonly done in cyclone separators. Additionally, in the illustrated embodiment, first section 9 includes second tangential inlet 13, which may be essentially similar to tangential inlet 10. Outer vessel space 8 has a smaller cross-sectional perimeter in second section 11 than in first section 9, which allows for a higher tangential velocity of the vortex flow in second section 11 during operation than in first section 9. In the illustrated embodiment, second section 11 includes lower tangential inlet 14, which may be used to introduce a liquid flow to further increase the tangential velocity of the vortex flow in second section 11.

[0041] The apparatus shown in FIG. 1 further includes an inner vessel 15 disposed within the outer vessel body 7. The inner vessel 15 includes an inner vessel body 16 having an inner vessel space 17 and an inner lower inlet 18 facing toward the lower end 4 of the outer vessel 1 and fluidly connecting the inner vessel space 17 with the outer vessel space 8. Additionally, in the illustrated configuration, the inner vessel 15 faces toward the upper end 2 of the outer vessel 1 and includes an inner upper outlet 19 fluidly connecting the inner vessel space 17 with the outer vessel space 8. A barrier 20 is disposed between the inner upper outlet 19 and the upper end 2 to at least partially block solids from entering the inner vessel space 17 while allowing fluids such as steam to exit through the inner upper outlet 19, for example, to be conveyed to the upper outlet 3. The apparatus further includes a traverse conduit 21 in fluid communication with the inner vessel space 17, which traverses the outer vessel body 7 and thereby conveys a product stream from the inner vessel space 17 to the exterior of the outer vessel.

[0042] For operation of the apparatus shown in FIG. 1 in the process of the present invention, a multiphase hydrocarbon stream 27, e.g., obtained from the depolymerization of plastic materials in a cracking reactor 26 as shown in FIG. 2, can be introduced into the outer vessel space 8 through the tangential inlet 10 and / or the second tangential inlet 13 to create a vortex. As a result of centrifugal force, solids and liquids are forced to the inner surface of the outer vessel body 7, while the vapor component is separated by moving radially inward and conveyed to the upper outlet 3. Preferably, the cross-sectional circumference of the first section 9 is sufficiently small to ensure that the axial velocity of the vapor product 30 moving toward the upper outlet 3 is sufficiently low to reduce droplet entrainment. The vapor product 30 discharged from the outer vessel space 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. The fluid can be obtained by condensing and recycling a portion of the recovered vapor product 30. The condensation step allows for preferential condensation of impurities having a higher boiling point than the desired components of vapor product 30, such as undesirable organophosphorus compounds commonly found in plastic materials. The condensed portion of vapor product 30 is returned to outer vessel space 8 and may be at least partially removed via solids-reduced product stream 25 and / or solids-enriched product stream 28.

[0043] After separation of the vapor product 30, the remaining hydrocarbon stream is conveyed from the first section 9 through the third section 12 to the second section 11, thereby increasing the tangential velocity of the vortex flow due to the reduced cross-sectional circumference. The increased tangential velocity shortens residence time, thereby reducing the tendency for coking. At the same time, the increased tangential velocity increases centrifugal force, thus resulting in more effective separation. This centrifugal force separates the hydrocarbon stream into a solids-enriched product stream 28 and a solids-reduced product stream 25. The solids-enriched product stream 28 is conveyed to the bottom outlet. The solids-reduced product stream 25 creates a liquid holdup in the outer vessel volume 8, thereby entering the inner vessel volume 17 through the inner bottom inlet 18 and ultimately reaching the traverse conduit 21, from where it can be recovered. Advantageously, the solids-reduced product stream enters the traverse conduit 21 at inlet opening 21 a and exits the traverse conduit 21 at outlet opening 21 b, which is located outside the outer vessel body 7 below inlet opening 21 a. Preferably, the traverse conduit 21 traverses the outer vessel body 7 at a position further below along the longitudinal axis 6 than the interior upper outlet 19 of the inner vessel 15.

[0044] Advantageously, the recovered solids-depleted product stream 25 may be recycled back to the cracking reactor 26 for further cracking. A solids-enriched product stream 28 may be recovered from the bottom outlet and fed to a further downstream separation step, such as a coke catcher 29. A portion of the solids-enriched product stream 28 may be recycled and introduced into the bottom tangential inlet 14 to further increase the tangential velocity of the vortex flow in the second section 11.

[0045] FIG. 2 illustrates a preferred embodiment of the application of the apparatus of the present invention in a plastics processing facility. Plastic material is fed to an extruder 23, where it is compressed, melted, and / or degassed. The molten plastic material, preferably at a temperature of 250°C to 280°C, is mixed in a static mixer 22 with an external solvent 24, preferably heavy oil, to reduce the viscosity of the plastic melt, and / or at least a portion of the solids-reduced product stream 25 obtained from the apparatus of the present invention. The resulting mixture is then conveyed to a cracking reactor 26, where the plastic is depolymerized, preferably at a temperature of 400°C to 440°C. From the cracking reactor 26, a multiphase hydrocarbon stream 27 is obtained, which is then introduced into the outer vessel 1 of the apparatus of the present invention through a tangential inlet 10, as described herein above. At least a portion of the solids-reduced product stream 25 obtained from the apparatus of the present invention can be recycled and fed to a new plastic melt, preferably together with the solvent 24. The solids-enriched product stream 28 is conveyed to a coke catcher 29 for removal of coke particles, and at least a portion of the resulting stream may be recycled and injected into the lower tangential inlet 14 of the apparatus of the present invention, as described above. The vapor product 30 obtained from the apparatus of the present invention is further separated into a light product 31, preferably having a boiling range of 35°C to 225°C, and a heavy product 32, preferably having a boiling range of 225°C to 410°C. A portion of the heavy product 32 may be recycled to spray nozzles 33 arranged to cool and condense a portion of the vapor product 30, as described hereinabove. The present disclosure also includes the following aspects. <1> 1. An apparatus for separating components of a multiphase hydrocarbon stream (27), said apparatus comprising: - an outer container (1) having an upper end (2) with an upper outlet (3), a lower end (4) with a lower outlet (5), and an outer container body (7) disposed between the upper end (2) and the lower end (4) and having an outer container interior space (8) in fluid communication with the upper outlet (3) and the lower outlet (5), the outer container having a longitudinal axis (6) extending between the upper end (2) and the lower end (4); The outer container body (7) is a first section (9) comprising a tangential inlet (10) arranged to introduce the multiphase hydrocarbon stream (27) tangentially into the outer vessel space (8) to create a vortex flow; and a second section (11) disposed closer to the lower end (4) than the first section (9), wherein the outer container space (8) has a smaller cross-sectional perimeter in the second section (11) than in the first section (9); an outer container (1); an inner container (15) arranged in the outer container body (7), the inner container (15) comprising: an inner container body (16) having an inner container space (17); - an inner lower inlet (18) facing towards the lower end (4) of the outer container (1) and in fluid communication with the inner container space (17) and the outer container space (8); an inner container (15) comprising: - a traverse conduit (21) in fluid communication with the inner vessel space (17) and traversing the outer vessel body (7); An apparatus comprising: <2> a ratio of the cross-sectional circumferential length of the outer container space (8) in the second section (11) to the cross-sectional circumferential length of the outer container space (8) in the first section (9) is 0.05 to 0.95, preferably 0.1 to 0.9, more preferably 0.25 to 0.8, even more preferably 0.4 to 0.7, and most preferably 0.5 to 0.6; <1> The device described in <3> a cooling system fluidly connected to the upper outlet (3), the cooling system configured to condense a portion of the vapor product (30) discharged from the outer vessel interior space (8) through the upper outlet (3) and convey the condensed portion of the vapor product (30) back to the outer vessel interior space (8), preferably the cooling system comprising at least one spray nozzle (33); <1> or <2> The device described in <4> the space within the outer container (8) in the first section (9) and / or the second section (11) is substantially cylindrical or substantially frustoconical, preferably substantially cylindrical; <1> ~ <3> 10. The device according to claim 9, wherein: <5> the first section (9) comprising a second tangential inlet (13) arranged to introduce the multiphase hydrocarbon stream (27) tangentially into the outer vessel space (8) to create a vortex flow; <1> ~ <4> 10. The device according to claim 9, wherein: <6> the second section (11) comprises a lower tangential inlet (14) arranged to introduce a flow tangentially into the outer vessel space (8); <1> ~ <5> 10. The device according to claim 9, wherein: <7> the inner container (15) has an inner upper outlet (19) facing the upper end (2) of the outer container (1) and in fluid communication with the outer container interior space (8) and the inner container interior space (17); and preferably, the traverse conduit (21) crosses the outer container body (7) at a position further below the inner upper outlet (19) of the inner container (15) along the longitudinal axis (6); <1> ~ <6> 10. The device according to claim 9, wherein: <8> the inner container (15) comprises a barrier (20) disposed between the inner upper outlet (19) and the upper end (2) of the outer container (1), the barrier (20) being disposed to at least partially block solids from entering the inner container space (17) through the inner upper outlet (19) but allowing fluids to exit the inner container space (17) through the inner upper outlet (19); <7> The device described in <9> <1> ~ <8> 1. A process for separating components of a multiphase hydrocarbon stream (27) in an apparatus according to any one of claims 1 to 9, wherein the process comprises: - introducing the multiphase hydrocarbon stream (27) through the tangential inlet (10) into the outer vessel volume (8) to create a vortex flow, whereby a vapor product (30) is separated from the hydrocarbon stream and conveyed to the top outlet (3); - recovering said vapor product (30) from said top outlet (3); - conveying 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 solids-depleted product stream (25), and the solids-enriched product stream (28) is conveyed to the bottom outlet (5); - recovering said solids-enriched product stream (28) from said bottom outlet (5); - conveying the solids-reduced product stream (25) through the inner vessel lower inlet (18) into the inner vessel space (17); and - withdrawing the solids-reduced product stream (25) from the inner vessel space (17) through the traverse conduit (21); The process includes: <10> the method further includes a step of condensing a portion of the vapor product (30) discharged from the outer container space (8) through the upper outlet (3) and transporting the condensed portion of the vapor product (30) back to the outer container space (8). <9> The process described in <11> the condensation is achieved by spraying a fluid onto the vapor product (30), the temperature of the fluid being lower than the temperature of the vapor product (30), preferably the temperature of the fluid is between 120°C and 350°C, preferably between 150°C and 300°C, in particular between 180°C and 250°C; <10> The process described in <12> the fluid is obtained by condensing and recycling a portion of the recovered vapor product (30); <11> The process described in <13> 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, and most preferably between 360°C and 400°C; <9> ~ <12> 10. The process according to any one of the preceding claims. <14> the multiphase hydrocarbon stream (27) is obtained from the depolymerization of plastic material, preferably plastic waste, <9> ~ <13> 10. The process according to any one of the preceding claims. <15> The plastic material comprises a polyolefin, preferably selected from polyethylene and polypropylene, and / or polystyrene; <14> The process described in <16> the multiphase hydrocarbon stream (27) contains impurities selected from aluminum powder and / or organophosphorus compounds, in particular tris(2,4-di-tert-butylphenyl)phosphite; <9> ~ <15> 10. The process according to any one of the preceding claims.

Claims

1. 1. An apparatus for separating components of a multiphase hydrocarbon stream (27), said apparatus comprising: - an outer container (1) having an upper end (2) with an upper outlet (3), a lower end (4) with a lower outlet (5), and an outer container body (7) arranged between said upper end (2) and said lower end (4) and having an outer container interior space (8) in fluid communication with said upper outlet (3) and said lower outlet (5), said outer container having a longitudinal axis (6) extending between said upper end (2) and said lower end (4), The outer container body (7) is a first section (9) comprising a tangential inlet (10) arranged to introduce said multiphase hydrocarbon stream (27) tangentially into said outer vessel space (8) to create a vortex flow; and a second section (11) arranged closer to the lower end (4) than the first section (9), wherein the outer container space (8) has a smaller cross-sectional perimeter in the second section (11) than in the first section (9); an outer container (1), an inner container (15) arranged in said outer container body (7), said inner container (15) comprising: an inner container body (16) having an inner container space (17); an inner lower inlet (18) pointing towards the lower end (4) of the outer container (1) and in fluid communication with the inner container space (17) and the outer container space (8); an internal upper outlet (19) pointing towards the upper end (2) of the outer container (1) and in fluid communication with the outer container interior space (8) and the inner container interior space (17); an inner container (15) comprising: a traverse conduit (21) in fluid communication with the inner vessel space (17) and crossing the outer vessel body (7), by which a product stream can be conveyed from the inner vessel space (17) to the outside of the outer vessel (1), the traverse conduit (21) crossing the outer vessel body (7) at a position further down along the longitudinal axis (6) than the inner upper outlet (19) of the inner vessel (15); An apparatus comprising:

2. 2. The device according to claim 1, wherein a ratio of the cross-sectional perimeter of the outer container space (8) in the second section (11) to the cross-sectional perimeter of the outer container space (8) in the first section (9) is between 0.05 and 0.

95.

3. 3. The apparatus of claim 1, further comprising a cooling system fluidly connected to the upper outlet (3), the cooling system configured to condense a portion of the vapor product (30) discharged from the outer vessel interior space (8) through the upper outlet (3) and to convey the condensed portion of the vapor product (30) back to the outer vessel interior space (8).

4. 3. The device according to claim 1 or 2, wherein the outer vessel space (8) in the first section (9) and / or the second section (11) is cylindrical or frusto-conical.

5. 3. The apparatus of claim 1 or claim 2, wherein the first section (9) comprises a second tangential inlet (13) arranged to introduce the multiphase hydrocarbon stream (27) tangentially into the outer vessel volume (8) to create a vortex.

6. 3. The apparatus according to claim 1 or claim 2, wherein the second section (11) comprises a lower tangential inlet (14) arranged to introduce a flow tangentially into the outer vessel space (8).

7. 3. The apparatus of claim 1 or claim 2, wherein the inner container (15) comprises a barrier (20) arranged between the inner upper outlet (19) and the upper end (2) of the outer container (1), the barrier (20) being arranged to at least partially block solids from entering the inner container space (17) through the inner upper outlet (19) but to allow fluids to exit the inner container space (17) through the inner upper outlet (19).

8. 3. A process for separating components of a multiphase hydrocarbon stream (27) in an apparatus according to claim 1 or claim 2, said process comprising: - introducing said multiphase hydrocarbon stream (27) through said tangential inlet (10) into said outer vessel space (8) to create a vortex flow, whereby a vapor product (30) is separated from said hydrocarbon stream and conveyed to said top outlet (3); - recovering said vapor product (30) from said top outlet (3); conveying 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 solids-depleted product stream (25), and the solids-enriched product stream (28) is conveyed to the bottom outlet (5), - recovering said solids-enriched product stream (28) from said bottom outlet (5), - conveying said solids-reduced product stream (25) through said inner lower inlet (18) into the inner vessel space (17); and - withdrawing said solids-reduced product stream (25) from said inner vessel space (17) through said traverse conduit (21); The process includes:

9. 9. The process of claim 8, further comprising the step of condensing a portion of the vapor product (30) discharged from the outer vessel interior space (8) through the upper outlet (3) and conveying the condensed portion of the vapor product (30) back to the outer vessel interior space (8).

10. 10. The process of claim 9, wherein the condensation is achieved by spraying a fluid onto the vapor product (30), the temperature of the fluid being lower than the temperature of the vapor product (30).

11. 11. The process of claim 10, wherein the fluid is obtained by condensing and recycling a portion of the recovered vapor product (30).

12. The process of claim 8, wherein the temperature of the multiphase hydrocarbon stream (27) at the tangential inlet (10) is between 300°C and 480°C.

13. 9. The process of claim 8, wherein the multiphase hydrocarbon stream (27) is obtained from the depolymerization of a plastic material.

14. 14. The process of claim 13, wherein the plastic material comprises a polyolefin and / or polystyrene.

15. 9. The process of claim 8, wherein the multiphase hydrocarbon stream (27) comprises impurities selected from aluminum powder and / or organophosphorus compounds.

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