Process and chemical plant for separating c6-c8 aromatic hydrocarbons from a liquid stream

Abstract

This invention relates to a method and chemical apparatus for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil manufactured from plastic waste. The liquid stream is converted in a first hydrotreating step, and then the stream containing C6-C8 aromatic hydrocarbons is separated from the hydrotreated liquid stream and subjected to a second hydrotreating step to produce a further hydrotreated stream from which the desired C6, C7, and C8 aromatic hydrocarbons are separated. The method and chemical apparatus according to the invention are suitable for avoiding undesirable polymerization and scaling.

Description

Technical Field

[0001] The present invention relates to a method and chemical apparatus for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil made from plastic waste. Background Technology

[0002] AU 2021 / 222788 A1 discloses a method for processing plastic pyrolysis oil, comprising steps a) selective hydrogenation, b) hydrotreating, and c) separating the hydrotreated effluent. At least a portion of the hydrotreated effluent obtained after separation in step c) is recycled to a) selective hydrogenation and / or b) hydrotreating. Selective hydrogenation (step a)) at temperatures up to 250°C may result in undesirable polymerization of the plastic pyrolysis oil portion within the hydrogenation unit. Furthermore, since the entire hydrotreated stream obtained in step a) is subjected to hydrotreating in step b), the separation steps following selective hydrogenation a) and hydrotreating b) require larger and therefore more expensive hydrotreating units. Additionally, H2 consumption is very high for the same reason. Separation by distillation is unsuitable for separating C6-C8 aromatics from the stream. Therefore, this method aims to produce steam cracking feedstock rather than a C6-C8 aromatics stream. The methods discussed above are... Figure 1 The examples shown are used as comparative examples in the Examples section of this invention.

[0003] Document US 10,975,313 B2 discloses a method for obtaining aromatics from pyrolysis oil. This method utilizes a first hydrocracking unit for mild hydrocracking, a reforming unit downstream of the first hydrocracking unit, and an aromatics separation unit downstream of the reforming unit. At least a portion of the non-aromatic stream obtained in the aromatics separation unit is recycled to the reforming unit. The disclosed method requires numerous separate process steps, including (mild) hydrocracking and reforming, resulting in a highly complex overall process.

[0004] Document US 2023 / 0287282 A1 discloses a method for purifying hydrocarbon streams, the method comprising a "hydrogenation treatment step". The method produces a purified hydrocarbon stream suitable as a feedstock for steam cracking.

[0005] Document WO 2023 / 052765 A1 discloses a method for upgrading high-olefin oil derived from waste plastic pyrolysis, wherein the high-olefin oil is mixed with hydrogen and a “saturated near-zero olefin stream” to form a “diluted feed stream,” which is then subjected to a two-stage process having at least two hydrotreating reactors. No distillation is applied between the at least two hydrotreating reactors.

[0006] Document WO 2018 / 058172 A1 discloses a process sequence of a) first hydrotreating, b) distillation, and c) second hydrotreating for treating biomass pyrolysis oil. Biomass-derived pyrolysis oils have a diverse composition, particularly lower levels of compounds with C / C double and / or C / C triple bonds, such as dienes, which are a major cause of undesirable scaling during comparable treatment of plastic pyrolysis oils. The recycle stream separated from the first hydrotreating effluent is not disclosed in this document.

[0007] The object of this invention is to provide a method and chemical apparatus for separating a stream of C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil obtained through the pyrolysis of plastic waste. Furthermore, when separating a stream of C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil obtained through the pyrolysis of plastic waste, the method and chemical apparatus should reduce undesirable scaling during the process. Summary of the Invention

[0008] These problems are addressed by a method for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil, the method comprising the following steps:

[0009] (i) Providing a liquid stream S1 comprising at least one plastic pyrolysis oil, the liquid stream S1 further comprising a C6-C8 aromatic hydrocarbon, an organic compound comprising at least one heteroatom, and a compound having a C-C double bond and / or a C-C triple bond.

[0010] (ii) Provide stream S2, which contains H2.

[0011] (iii) The liquid stream S1 and the liquid stream S2 are fed into the hydrogenation unit HU1, in which at least a portion of the components of the liquid stream S1 reacts with the liquid stream S2 in a hydrogenation reaction to form a liquid stream S3, wherein the liquid stream S3 is depleted relative to the liquid stream S1 of compounds having C-C double bonds and / or C-C triple bonds, and

[0012] Optionally, at least a portion of the liquid recirculation stream S3' is fed into the hydrogenation unit HU1, and the liquid recirculation stream S3' is separated from the liquid stream S3. Preferably, the mass ratio of "liquid recirculation stream S3' : liquid stream S3" preferably ranges from about 1 : 1 to about 30 : 1, more preferably from about 5 : 1 to about 20 : 1, and most preferably from about 10 : 1 to about 15 : 1.

[0013] (iv) At least a portion or the remainder of the liquid stream S3 is subjected to a distillation unit DU, in which at least a portion or the remainder of the stream S3 is separated into a stream S4 containing valuable products and a liquid stream S5, wherein the stream S4 containing valuable products comprises C6-C8 aromatic hydrocarbons and organic compounds containing at least one heteroatom.

[0014] (v) The stream S4 containing the valuable product is subjected to a hydrogenation unit HU2, in which the stream S4 is converted into a stream S6, wherein the stream S6 contains C6-C8 aromatic hydrocarbons and is relatively lean compared to stream S4, containing at least one heteroatom and / or C / C double bond of an organic compound, and

[0015] (vi) Separate C6-C8 aromatic hydrocarbons from stream S6 in the aromatic hydrocarbon extraction unit AEU.

[0016] These problems are further addressed by a chemical apparatus for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil.

[0017] (i) at least one first hydrogenation processing unit HU1, the at least one first hydrogenation processing unit HU1

[0018] It contains at least one entrance and at least one exit.

[0019] (ii) Optionally, a recirculation unit is located downstream of the inlet and outlet of the first hydrogenation treatment unit HU1 and is fluidly connected to the inlet and outlet of the first hydrogenation treatment unit HU1.

[0020] (iii) A distillation unit DU, which is downstream of and fluidly connected to the outlet of the first hydrogenation treatment unit HU1, the distillation unit DU having a bottom outlet BO and a top outlet HO.

[0021] (iv) A second hydrogenation treatment unit HU2, which is downstream of the top outlet HO of the distillation unit DU and is fluidly connected to the top outlet HO of the distillation unit DU.

[0022] (v) At least one aromatic hydrocarbon extraction unit AEU, which is downstream of and fluidly connected to the second hydrogenation treatment unit HU2. Attached Figure Description

[0023] Figure 1 A method is shown in which a recycle stream from the second hydrogenation unit into the first hydrogenation unit is utilized. This recycle stream is used in the method disclosed in AU 2021 / 222788 A1 and is therefore used as a comparative example in the Examples section.

[0024] Figure 2 The present invention illustrates a method and chemical apparatus for separating C6-C8 aromatic hydrocarbon streams from a liquid stream containing at least one type of plastic pyrolysis oil.

[0025] Figure 3 Further aspects of the method and chemical apparatus according to the invention for separating C6-C8 aromatic hydrocarbon streams from a liquid stream containing at least one type of plastic pyrolysis oil are shown. Detailed Implementation

[0026] The present invention is further described below with reference to embodiments, but the present invention is not limited to these embodiments, and any modifications or substitutions to these embodiments or combinations thereof within the basic spirit of the present invention are still within the scope of the present invention as claimed.

[0027] definition:

[0028] In the context of this specification and the appended claims, the term "about" preferably means a deviation of ±10% from the value described therein. In the context of this invention, the term "combination thereof" includes one or more of the listed elements. In the context of this invention, the term "mixture thereof" includes one or more of the listed elements.

[0029] In the context of this invention, the term "pyrolysis" refers to the thermal decomposition or degradation of a raw material, such as plastic waste, under inert conditions, producing gaseous, liquid, and solid char components. During pyrolysis, the raw material is converted in a pyrolysis unit into a wide variety of chemicals, including gases such as H2, C1- to C4-alkanes, C2- to C4-olefins, acetylene, propyne, 1-butyne, plastic pyrolysis oil having a boiling temperature of 25°C to 500°C or higher, and char. The direct products from this pyrolysis are "pyrolysis gases" and solid products. The liquid product, "pyrolysis oil," is then separated from the "pyrolysis gases" by condensation. Furthermore, water is formed during pyrolysis, which may be partially dispersed in the pyrolysis oil and may be partially contacted with the pyrolysis oil as a separate phase. The water formed during pyrolysis contains various organic compounds and / or their salts that are also formed during pyrolysis. The term "pyrolysis" includes slow pyrolysis, fast pyrolysis, flash catalytic pyrolysis, and catalytic pyrolysis. These pyrolysis types differ in process temperature, heating rate, residence time, and feed particle size, resulting in varying product qualities. Pyrolysis units can operate adiabatic, isothermal, non-adiabatic, non-isothermal, or combinations thereof. The pyrolysis reaction disclosed herein can be carried out in a single stage or in multiple stages. For example, a pyrolysis unit may comprise two reactor vessels connected in series with fluid connection.

[0030] In the context of this invention, "valuable component" means "C6-C8 aromatic hydrocarbons" (benzene, toluene, 1,2-xylene, 1,3-xylene, 1,4-xylene, and ethylbenzene).

[0031] In the context of this invention, the term "plastic pyrolysis oil" should be understood to mean any oil derived from the pyrolysis of plastic waste. The term "plastic waste" includes rubber waste such as scrap tires and raw materials containing plastic waste. Plastic pyrolysis oil is obtained and / or is available from the pyrolysis of such plastic waste. Pyrolysis oil produced from pyrolyzed plastic waste differs, for example, in composition from pyrolysis oil produced from fossil raw materials that do not contain plastic waste.

[0032] In the context of this invention, the term "plastic waste" refers to any plastic material that is discarded after use, i.e., the plastic material has reached the end of its service life and is considered post-consumer waste. Plastic waste can be pure polymer plastic waste, mixed plastic waste, or membrane waste, including sludge, adhesive materials, fillers, residues, etc. Plastic waste may have oxygen content, nitrogen content, sulfur content, halogen content, and optionally heavy metal content. Plastic waste can originate from any source containing plastic materials.

[0033] Therefore, the term "plastic waste" includes industrial and household plastic waste, as well as used tires and agricultural and horticultural plastic materials.

[0034] Typically, plastic waste is a mixture of different plastic materials, including hydrocarbon plastics such as polyolefins such as polyethylene (HDPE, LDPE) and polypropylene, polystyrene and their copolymers, and polymers composed of carbon, hydrogen and other elements such as chlorine, fluorine, oxygen, nitrogen, sulfur, silicon, etc., such as chlorinated plastics such as polyvinyl chloride (PVC), polyvinylidene chloride (PVDC), nitrogen-containing plastics such as polyamide (PA), polyurethane (PU), acrylonitrile butadiene styrene (ABS), oxygen-containing plastics such as polyesters such as polyethylene terephthalate (PET), polycarbonate (PC), silicone and / or sulfur-bridged crosslinked rubber.

[0035] Typically, plastic materials contain additives such as processing aids, plasticizers, flame retardants, pigments, light stabilizers, lubricants, impact modifiers, antistatic agents, antioxidants, etc. These additives may contain elements other than carbon and hydrogen. For example, the presence of bromine is primarily associated with flame retardants. Heavy metal compounds can be used as light-resistant pigments and / or stabilizers in plastics. Cadmium, zinc, and lead may be present in heat stabilizers and slip agents used in plastic manufacturing. Plastic waste may also contain residues. In the context of this invention, residues are contaminants that adhere to plastic waste. Additives and residues are generally present in amounts of less than 50 wt.-%, preferably less than 30 wt.-%, more preferably less than 20 wt.-%, and even more preferably less than 10 wt.-%, based on the total dry weight of the plastic.

[0036] Examples of rubber waste (also considered "plastic waste" in the context of this invention) include end-of-life tires, rubber waste generated during the manufacturing process, and discarded rubber-containing products such as latex inspection gloves and gaskets. End-of-life tires contain additional components, such as textiles and organic and inorganic additives, which can be separated from the rubber portion of the end-of-life tire before pyrolysis. The pyrolysis oil obtained by (primarily) the pyrolysis of end-of-life tires is also known as tire pyrolysis oil (TPO) and is "plastic pyrolysis oil" in the context of this invention.

[0037] Examples of biological waste that can be included in “plastic waste” include green waste, food waste, human waste, manure, sewage, sewage sludge and slaughterhouse waste.

[0038] To obtain the plastic pyrolysis oil according to the invention, the feedstock is inserted into the pyrolysis reactor using a metering unit such as a screw or extruder, a rotary valve, a pneumatic conveyor, or a liquid injector. The feedstock may optionally be preheated in, for example, a heat exchanger and / or subjected to pre-pyrolysis at a temperature, for example, in the range of about 200°C to about 360°C, before being inserted into the pyrolysis reactor. The feedstock is then heated in the pyrolysis reactor to a temperature in the range of about 350°C to about 900°C, more preferably in the range of 400°C to about 550°C, and a pressure in the range of about 0.5 bar to about 2 bar (absolute value), more preferably in the range of 0.9 bar to about 1.5 bar (absolute value). The pyrolysis reactor is preferably selected from the group consisting of fluidized bed reactors, moving bed reactors, entrained flow reactors, screw reactors, extruders, stirred tank reactors, and rotary kiln reactors. Preferably, the pyrolysis is carried out in the pyrolysis reactor under an inert atmosphere free of oxygen or air.

[0039] Pyrolysis methods are known in themselves. They are described, for example, in EP 0713906 A1 and WO 95 / 03375 A1. Suitable plastic pyrolysis oils are also commercially available. Plastic pyrolysis oils are typically liquid at 15°C or waxy at said temperature. In the terminology of this invention, "liquid at 15°C" means that the plastic pyrolysis oil has a density of at most 1.3 g / ml at 15°C and 1013 mbar, as determined according to DIN EN ISO 12185, for example, a density in the range of 0.65 to 0.98 g / ml.

[0040] The amount of C6-C8 aromatics formed by the pyrolysis reaction of the above-mentioned feedstock can be increased, for example, in the presence of a suitable catalyst. Another suitable method for increasing the amount of C6-C8 aromatics is disclosed in EP 3744814 A1: the pyrolysis gas obtained from the pyrolysis reaction of the above-mentioned feedstock is then subjected to thermal catalytic treatment at about 450°C to about 600°C (at least 50°C lower than the pyrolysis reaction temperature applied in the first step) in the presence of an aromatization catalyst such as ZSM-5, ZSM-11, ZSM-35, ZSM-23, magnesium alkali zeolite, β-zeolite, zeolite Y, zeolite X, mordenite, zeolite A, IM-5, SSZ-20, SSZ-55, MCM-22, TNU-9, metal-treated, exchanged, or impregnated catalysts, and combinations of the aforementioned catalysts and post-treatments. Other suitable catalysts include sand and alumina. Furthermore, combinations of the above-mentioned catalysts can be used for this purpose.

[0041] The amount of C6-C8 aromatic hydrocarbons in plastic pyrolysis oil can also be increased by reforming the plastic pyrolysis oil or a mixture thereof (e.g., by catalytic reforming). Such reforming reactions are disclosed, for example, at https: / / www.e-education.psu.edu / fsc432 / content / catalyic-reforming-processes

[0042] And if necessary, adjustments can be made by technicians.

[0043] A liquid stream S1 containing plastic pyrolysis oil or a mixture of plastic pyrolysis oil can also be produced by pyrolysis of a plastic waste stream containing polystyrene. The liquid stream S1 further contains C6-C8 aromatic hydrocarbons, organic compounds containing at least one heteroatom, and compounds having C-C double bonds and / or C-C triple bonds (Maafa, IM Pyrolysis of Polystyrene Waste: A Review. Polymers 2021, 13, 225. https: / / doi.org / 10.3390 / polym13020225).

[0044] The liquid stream S1, more preferably the at least one plastic pyrolysis oil contained in the liquid stream S1, comprises at least 5 wt.-%, or at least 10 wt.-%, or at least 15 wt.-%, or at least 20 wt.-%, or at least 25 wt.-%, or at least 30 wt.-%, or at least 35 wt.-%, or at least 40 wt.-%, or at least 45 wt.-%, or at least 50 wt.-%, or at least 55 wt.-%, or at least 60 wt.-%, or at least 70 wt.-%, or at least 80 wt.-%. Preferably, the C6-C8 aromatic hydrocarbons are selected from the group consisting of benzene, toluene, 1,2-xylene, 1,3-xylene, 1,4-xylene, and ethylbenzene.

[0045] The at least one plastic pyrolysis oil contained in liquid stream S1 preferably further has a bromine value of about 2 g Br2 / 100 g to about 150 g Br2 / 100 g (as determined by ASTM 1159) and / or a C5 hydrocarbon content of about 0.03 wt.-% to about 12.2 wt.-% (as determined by ASTM D 5134) and / or a naphthalene content of about 0.5 wt.-% to about 18.4 wt.-% (as determined by ASTM D 5134) and / or a styrene content of about 0.02 wt.-% to about 29.5 wt.-% (as determined by ASTM D 5134) and / or a toluene content of about 4.3 wt.-% to about 71.5 wt.-% (as determined by ASTM D 5134). Such plastic pyrolysis oils are particularly suitable for the methods and chemical equipment according to the invention.

[0046] Optionally, before being used as the liquid stream S1 in the method according to the invention and / or as a feedstock for the chemical equipment according to the invention, the plastic pyrolysis oil or a mixture of plastic pyrolysis oils may be subjected to one or more methods selected from filtration, centrifugation, adsorption, washing, and extraction. Such optional pretreatment methods are described, for example, in WO 2021 / 224287 A1, WO 2023 / 061834 A1, EP 0713906 A1, and WO 95 / 03375 A1, which are incorporated herein by reference. Those skilled in the art will understand how and in what circumstances the pretreatment methods disclosed in the aforementioned documents and comparable pretreatment methods disclosed elsewhere may be used.

[0047] Liquid stream S1 comprises at least one plastic pyrolysis oil produced by the above-described raw materials and the above-described method or a mixture of such plastic pyrolysis oils. Liquid stream S1 comprises C6-C8 aromatic hydrocarbons, organic compounds containing at least one heteroatom, and compounds having C-C double bonds (olefins, dienes) and / or C-C triple bonds, contributed by the at least one plastic pyrolysis oil optionally included in liquid stream S1 and / or additional liquid hydrocarbon feedstocks. Examples of such additional liquid hydrocarbon feedstocks are further given below.

[0048] In step (i) of the method according to the invention, a liquid stream S1 comprising at least one plastic pyrolysis oil is provided, the liquid stream S1 further comprising C6-C8 aromatic hydrocarbons, an organic compound comprising at least one heteroatom, and a compound having a C-C double bond and / or a C-C triple bond. Figure 2 and 3 Liquid stream S1 may further comprise at least one additional liquid hydrocarbon feedstock comprising C6-C8 aromatic hydrocarbons different from those obtained from the pyrolysis of plastic waste. Suitable examples of such additional liquid hydrocarbon feedstocks include pyrolysis gasoline and coke oven light oil (CAS No.: 65996-78-3). Pyrolysis gasoline is obtained or is a byproduct of the steam cracking of hydrocarbon feedstocks, such as naphtha. Pyrolysis gasoline and its production are known in the art. Pyrolysis gasoline comprises C6-C8 aromatic hydrocarbons. Coke oven light oil can be obtained by extraction from gases escaping from the destructive distillation of coal at high temperatures (e.g., above 700°C). It consists primarily of benzene, toluene, and xylene and may contain other minor hydrocarbon components.

[0049] This additional liquid hydrocarbon feedstock (the sum of all liquid hydrocarbon feedstocks in the case of more than one liquid hydrocarbon feedstock) may, for example, be included in liquid stream S1 in an amount of 0 wt.-%, 5 wt.-%, 10 wt.-%, 15 wt.-%, 20 wt.-%, 25 wt.-%, 30 wt.-%, 35 wt.-%, 40 wt.-%, 45 wt.-%, 50 wt.-%, 55 wt.-%, 60 wt.-%, 65 wt.-%, 70 wt.-%, 75 wt.-%, 80 wt.-% or greater, provided that at least 2 wt.-% of liquid stream S1 consists of at least one plastic pyrolysis oil produced by the pyrolysis of plastic waste.

[0050] In step (ii) of the method according to the invention, a stream S2 containing H2 is provided. Stream S2 may consist substantially of H2 or contain H2 along with at least one other gas. Preferably, the H2 content of stream S2 is greater than about 50% by volume, more preferably greater than about 80% by volume, and most preferably greater than about 95% by volume. This minimizes the amount of purge gas required to maintain a high H2 partial pressure and conserves H2. A high H2 partial pressure promotes catalyst activity and allows for a low reaction temperature. The advantage of a low reaction temperature is that undesirable polymerization of the components in stream S2 is suppressed. Such polymerization leads to undesirable scaling during processing.

[0051] The hydrogen (H2) used in the methods and systems according to the invention is preferably “green hydrogen” generated, for example, through water electrolysis and / or methane pyrolysis using electricity generated from renewable energy sources (e.g., solar, wind, tidal, and nuclear) and / or low-carbon energy sources, preferably at least partially from methane pyrolysis from renewable sources. Methane from renewable sources includes biomethane.

[0052] Optionally, at least a portion of the hydrogen used in the method according to the invention is hydrogen formed during the pyrolysis reaction and separated from the volatile pyrolysis reaction products.

[0053] In step (iii) of the method according to the invention, a compound having C-C double bonds and / or C-C triple bonds present in liquid stream S1 is hydrogenated in the first hydrogenation treatment unit HU1 in the presence of stream S2. This forms a liquid stream S3 exiting the first hydrogenation treatment unit HU1. Optionally and preferably, a portion of liquid stream S3 is separated from liquid stream S3 and fed into the first hydrogenation treatment unit HU1 as a liquid recycle S3' together with liquid streams S1 and S2.

[0054] The first hydrogenation treatment unit HU1 includes at least one stage in which CC double bonds and / or CC triple bonds present in the liquid stream S1 are hydrogenated. The first hydrogenation treatment unit HU1 is preferably a three-phase reactor, more preferably a three-phase reactor having a fixed catalyst bed. The three-phase reactor is most preferably operated in a trickle flow mode or a pulse flow mode. The fixed catalyst bed preferably contains at least one catalyst used in at least one stage of the first hydrogenation treatment unit HU1. The first hydrogenation treatment unit HU1 may also contain two or more such reactors, or a single reactor may contain one or more beds, each containing one or more catalysts.

[0055] Preferably, the first hydrogenation treatment unit HU1 comprises a single reactor with a single catalyst bed. This minimizes the geometry of the first hydrogenation treatment unit HU1 and ensures a cost-effective reactor design.

[0056] The at least one hydrogenation reactor of the first hydrogenation treatment unit HU1 is preferably designed to operate in a trickle or pulse flow mode, wherein the gas phase (gas flow S2 containing H2) is continuous or semi-continuous, and the liquid phase (liquid flow S1) flows along the surface of the solid, mainly along the surface of the at least one catalyst, thereby efficiently wetting them.

[0057] The process temperature in the at least one hydrogenation reactor of the first hydrogenation treatment unit HU1 depends on the type and activity of the catalyst used. The process temperature preferably ranges from about 60°C to about 250°C, more preferably from about 60°C to about 200°C, and most preferably from about 80°C to about 120°C. Catalyst deactivation can optionally be compensated for by increasing the process temperature.

[0058] In the at least one hydrogenation reactor of the first hydrogenation treatment unit HU1, the hydrogen pressure is preferably in the range of about 1.0 to about 10 MPa (absolute value).

[0059] The weight time space velocity (WHSV) of the liquid flow S1, excluding the optional liquid recirculation flow S3', is preferably in the range of about 0.1 t / (m²). 3 Kat. •h) to approximately 5 t / (m 3 Kat. •h), more preferably about 0.5 t / (m 3 Kat. •h) to approximately 1.0 t / (m 3 Kat. •h).

[0060] The method disclosed in WO 2018 / 058172 A1 does not include liquid recirculation S3'. The technical effects of the liquid recirculation S3' present in the method according to the present invention are described as follows:

[0061] The selected process conditions allow the liquid stream S1 to be maintained in the liquid phase during step (iii). The amount of hydrogen contained in the first hydrogenation treatment unit HU1 is sufficient to hydrogenate the undesirable C-C double bonds (olefins, dienes) and C-C triple bonds present in the liquid stream S1, but insufficient to hydrogenate the desired C6-C8 aromatic hydrocarbons also present in the liquid stream S1 by cyclic hydrogenation.

[0062] The optional liquid recirculation flow S3' dilutes the liquid flow S1, further reducing unwanted scaling caused by polymerization within the first hydrogenation treatment unit HU1. Furthermore, when the optional liquid recirculation flow S3' dilutes the liquid flow S1, the temperature inside the first hydrogenation treatment unit HU1 can be better controlled.

[0063] The ratio “liquid recirculation flow S3´ : liquid flow S1” preferably ranges between about 2 : 1 and about 20 : 1, more preferably between about 8 : 1 and about 15 : 1.

[0064] Preferably, the liquid stream S1 and the optional recirculated liquid stream S3' are mixed before entering the at least one reactor of the first hydrogenation treatment unit HU1.

[0065] Preferably, a suitable catalyst for the first hydrogenation treatment unit HU1 comprises at least one catalytically active metal selected from elements of groups 8 to 12 of the periodic table, more preferably selected from or composed of the group consisting of nickel, palladium, platinum, and rhodium, and most preferably palladium. When palladium is the catalytically active metal, the catalyst comprises palladium in an amount (calculated as elemental palladium) ranging from about 0.01 wt.-% to about 5 wt.-%, more preferably from about 0.1 wt.-% to about 1 wt.-%, and most preferably from 0.15 wt.-% to 0.8 wt.-% based on the total weight of the catalyst.

[0066] Suitable catalysts further comprise a support, preferably an inorganic support, such as silica, alumina, silica-alumina, silica-alumina phosphate, magnesium oxide, clay, carbon, and mixtures thereof. The support may also comprise a support-dopant, such as zirconium dioxide, cerium dioxide, titanium dioxide, and mixtures thereof. "Silica-alumina" also includes zeolite.

[0067] Preferably, the catalyst for the first hydrogenation treatment unit HU1 further comprises a promoter, more preferably one or more elements of Groups 10 and 11 of the periodic table, preferably one or more of copper, gold, silver and platinum, more preferably one or more of silver and platinum, and most preferably silver.

[0068] Preferably, the at least one catalytically active element is from Groups 8 to 12 of the periodic table, more preferably comprising or consisting of the group consisting of nickel, palladium, platinum, and rhodium, and most preferably the atomic ratio of palladium to the promoter is in the range of 0.1:1 to 10:1, more preferably 2:1 to 7:1, and more preferably 2.5:1 to 6:1.

[0069] Most preferably, the catalyst for the first hydrogenation treatment unit HU1 comprises palladium supported on a support material, preferably as defined above, wherein the support material is more preferably alumina or carbon, most preferably alumina.

[0070] In the context of this invention, the at least one catalyst used in the first hydrogenation treatment unit HU1 is preferably in the form of an extrusion, granules, rings, spherical particles or spheres, more preferably earth-shaped particles or extrusions.

[0071] Particle size here refers to particle size distribution, which is measured, for example, by sieving, laser diffraction, or other methods known in the art. Catalysts with desired particle size and optionally desired shape can be manufactured and used.

[0072] The catalyst used in the first hydrogenation unit HU1 (most preferably containing palladium or composed of palladium) is preferably activated at about 50°C to about 130°C under a hydrogen gas flow (e.g., GHSV = 1000 / h) for, for example, about 6 h to about 24 h, such as about 12 h, preferably under atmospheric conditions. When the catalyst is reduced in a larger reactor, the hydrogen gas can be diluted with nitrogen to avoid excessively high temperatures.

[0073] The height and diameter of the at least one catalyst bed are selected based on reaction kinetics, optimal liquid / gas flow patterns, and pressure drop. The at least one catalyst bed may consist of one or more layers of different solid absorbent materials, and / or one or more hydrogenation catalysts. The catalyst layers in the at least one catalyst bed may differ from each other in terms of particle size, shape, activity, or active sites. When using more than one catalyst bed, inert particles may be used above and below each bed to improve fluid distribution.

[0074] In the case where the at least one hydrogenation reactor in the first hydrogenation treatment unit HU1 has at least two stages, the catalyst preferably has different particle sizes in the at least two stages and / or optionally different shapes in the at least two stages.

[0075] Hydrogenation is an exothermic reaction and therefore each stage of the reaction can be optionally cooled.

[0076] Preferably, at least a portion of the liquid stream S3 is fed into the first hydrotreating unit HU1 as a recirculation stream S3' for at least a second time. In this case, the first hydrotreating unit HU1 preferably also includes a recirculation unit in which a desired portion of the optional recirculation stream S3' can be separated from the liquid stream S3. Before entering the first hydrotreating unit HU1, the liquid stream S1 is diluted with the optional recirculation stream S3', and thereby, undesirable scaling caused by the polymerization of compounds (olefins, dienes) with C / C double bonds and compounds with C / C triple bonds present in the liquid stream S1 is reduced.

[0077] The reactor inlet temperature of the first hydrotreating unit HU1 is optionally and preferably adjusted by mixing the warm liquid recirculation stream S3' and the cooled liquid recirculation stream S3' from the outlet of the at least one reactor of the first hydrotreating unit HU1 with the liquid stream S1 to adjust the desired reactor inlet temperature. This optional and preferred design avoids contact with the heat exchange surface, and thus avoids undesirable fouling on the heat exchanger surface, which would also lead to reduced heat transfer inside the heat exchanger, which is avoided by the optional and preferred design. If the outlet stream of the at least one reactor of the first hydrotreating unit HU1 is not warm enough, the polymerization stabilization portion of the liquid stream S3 is heated by the heat exchanger to adjust the necessary temperature.

[0078] About 90% or more, preferably more than 95% and most preferably 99% of the diene present in the liquid stream S1 is converted in step (iii) of the method according to the invention.

[0079] To maintain a high H2 partial pressure in the first hydrogenation treatment unit HU1, the first hydrogenation treatment unit HU1 is preferably operated with an exhaust gas stream S2'. More preferably, the H2 concentration in stream S2 is below 99.9% by volume to avoid the accumulation of inert gas components such as N2, CH4, and C2H6 in stream S2. The ratio of "H2 content in fresh H2 feed stream S2 : chemical H2 consumption caused by hydrogenation reaction in the first hydrogenation treatment unit HU1" is preferably in the range of about 1:1 to about 5:1, more preferably about 1:1 to about 3:1, and most preferably about 1:1 to about 2:1.

[0080] The total pressure at the outlet of the at least one reactor in the first hydrogenation treatment unit HU1 is preferably in the range of about 5 bar (absolute value) to about 60 bar (absolute value), more preferably about 10 bar (absolute value) to about 40 bar (absolute value), and most preferably about 20 bar (absolute value) to about 40 bar (absolute value).

[0081] Next, in step (iv) of the method according to the invention, at least a portion or the remainder of liquid stream S3 is distilled at high temperature in distillation unit DU to separate the at least a portion or the remainder of liquid stream S3 into stream S4 rich in valuable components (mononuclear aromatic components such as benzene, toluene, ethylbenzene, and xylene, i.e., C6-C8 aromatic hydrocarbons) and liquid stream S5 having a higher boiling point range than stream S4. Stream S4 contains at least a portion of C6-C8 aromatic hydrocarbons and organic compounds containing at least one heteroatom, which are contained in a portion of liquid stream S3. "The remainder of liquid stream S3" means the remainder of stream S3 after stream S3' is optionally separated from it in step (iii). Stream S4 preferably has a final boiling point of about 100°C to about 220°C, more preferably about 120°C to about 190°C, and most preferably about 150°C to about 170°C. Stream S4 also refers to "light stream" and stream S5 refers to "heavy stream".

[0082] Liquid stream S5 preferably has the same final boiling point as liquid stream S1. Liquid stream S5 can then be converted into syngas, primarily a mixture of H2 and CO, for example, in at least one vaporizer and / or partial oxidation reaction unit. Such partial oxidation reactions are known in the art and are disclosed, for example, in WO 2022 / 200532 A1, which is incorporated herein by reference. Those skilled in the art can select suitable reactors and reaction conditions to convert liquid stream S5 into syngas via partial oxidation and / or vaporization.

[0083] The final boiling points of streams S1, S3, S4, S5 and S6 are preferably measured by the methods described in ASTM D86 and ASTM D7169, and for very high boiling point liquids, also by ASTM D7182.

[0084] The distillation unit DU includes at least one distillation column, at least one thin-film evaporator, or a combination thereof. The distillation unit DU is downstream of and fluidly connected to the first hydrogenation treatment unit HU1. Preferably, the distillation unit DU includes or is composed of a distillation column.

[0085] Distillation is carried out at a temperature ranging from about 0°C to about 600°C, more preferably from about 20°C to about 400°C, and most preferably from about 80°C to about 250°C (the temperature range relates to an atmospheric pressure of 1.013 bar). The corresponding operating pressure of the at least one distillation column preferably ranges from about 0.001 bar to about 4 bar (absolute value), more preferably from about 0.001 bar to about 2.0 bar (absolute value), and most preferably from about 0.9 bar to about 1.8 bar (absolute value). When the pressure is ≠ 1.013 bar, the temperature is adjusted accordingly.

[0086] Optionally, the distillation unit DU includes at least one thin-film evaporator. In the thin-film evaporator, the medium to be evaporated or the solution to be concentrated by evaporation is applied as a thin film to the evaporator region. Thus, short contact times with the heated surface are feasible, and thermally unstable liquids and substances can be evaporated separately in such thin-film evaporators. Furthermore, if the product accumulating as residue has poor flow characteristics and / or is prone to aggregation, the thin-film evaporator can be used for separation tasks. The thin-film evaporation process is based on the principle of simple distillation, according to which the separation capacity of evaporators of this type is limited. Suitable thin-film evaporators are available in various designs, such as falling film evaporators or rotary evaporators.

[0087] Next, during step (v) of the method according to the invention, the stream S4 containing valuable components is converted in the second hydrogenation treatment unit HU2 into a purified stream S6 and a gas stream S6' containing valuable components. By hydrogenating the gas stream S4' containing hydrogen (H2) in the second hydrogenation treatment unit HU2, the purified stream S6 containing valuable components is depleted of heteroatoms such as nitrogen, oxygen, halogens (fluorine, chlorine, bromine, iodine), and sulfur relative to the stream S4. Optionally, the waste gas stream S2' can be fed into the second hydrogenation treatment unit HU2. In this case, the stream S4' balances the hydrogen demand of the second hydrogenation treatment unit HU2. Heteroatoms exit the second hydrogenation treatment unit HU2 as gas stream S6' in the form of their corresponding hydrides.

[0088] The corresponding hydrides of heteroatoms include NH3, H2O, H(Hal) (HF, HCl, HBr, HI), and H2S. NH3 and H(Hal) can form salts of the NH4Hal type (NH4F, NH4Cl, NH4Br, NH4I), and NH3 and H2S can form the salt NH4SH. Such salts may have already formed in the gas phase in the second hydrogenation unit HU2, and can then form undesirable deposits on the metal surface by resublimation when stream S6 cools.

[0089] NH4Cl, NH4F, NH4Br, NH4I, and NH4SH (at least one of which can be formed primarily in the second hydrogenation treatment unit HU2 (and a small portion may also be formed in the first hydrogenation treatment unit HU1)) are preferably removed from the second hydrogenation treatment unit HU2 by water. More preferably, NH4F, NH4Cl, NH4Br, NH4I, and / or the corresponding cations and anions are quantitatively removed by water, and NH4SH and / or the corresponding cations and anions are partially removed from the second hydrogenation treatment unit HU2 by a water stream. Figure 2 and 3 (Not shown in the image).

[0090] Therefore, the reactions in the second hydrogenation treatment unit HU2 include hydrodenitrogenation, hydrodeoxygenation, hydrodehalogenation, and hydrodesulfurization. Furthermore, the reactions include hydrodemetallization, and preferably, hydrogenation of the remaining C-C double bonds (olefins and dienes) and C-C triple bonds, while the conjugated C-C bonds in the C6-C8 aromatics present in the gas stream S4 are substantially not hydrogenated by the cyclohydrogenation in the second hydrogenation treatment unit HU2.

[0091] The second hydrogenation unit HU2 is downstream of the distillation unit DU and is fluidly connected to the distillation unit DU.

[0092] The second hydrotreating unit HU2 can be any vessel configured to contain the hydrotreating catalyst disclosed herein. The vessel is preferably configured for gas-phase operation. The second hydrotreating unit HU2 may include beds of one or more hydrotreating catalysts, preferably in a fixed-bed configuration. The second hydrotreating unit HU2 can operate adiabatically, isothermally, non-adiabatically, non-isothermally, or a combination thereof. The second hydrotreating unit HU2 may contain more than one vessel. Each of such vessels is considered a hydrogenation reactor.

[0093] The stream S4 containing valuable components can be contacted with the hydrotreating catalyst in an upward, downward, radial, or combination thereof, with or without the staged addition of gas stream S4, gas stream S2', or combinations thereof.

[0094] Preferably, heteroatoms containing halogens (such as chlorine), nitrogen, oxygen, and sulfur are removed from the stream S4 containing valuable components in the second hydrogenation treatment unit HU2. These heteroatoms are separated from organic residues, such as HF, HCl, HBr, NH3, H2O, and H2S, by hydrogenation treatment conditions, and the separated heteroatoms are replaced by hydrogen atoms in the organic residues. Furthermore, the remaining olefins and / or dienes in the stream S4 containing valuable components that were not converted to saturated hydrocarbons in the first hydrogenation unit HU1 are converted to saturated hydrocarbons in the second hydrogenation treatment unit HU2.

[0095] The hydrotreating catalyst can be any catalyst used for the hydrogenation of olefins, dienes, and heteroatom hydrogenation (e.g., commercially available hydrotreating catalysts). For this purpose, suitable hydrotreating catalysts include molybdenum catalysts (Mo catalysts), cobalt-molybdenum catalysts (Co-Mo catalysts), nickel-molybdenum catalysts (Ni-Mo catalysts), tungsten-molybdenum catalysts (W-Mo catalysts), cobalt-molybdenum oxides, nickel-molybdenum oxides, tungsten-molybdenum oxides, cobalt-molybdenum sulfides, nickel-molybdenum sulfides, tungsten-molybdenum sulfides, and molybdenum sulfides. Suitable catalysts further include a support, preferably an inorganic support, such as silica, alumina, silica-alumina, magnesium oxide, clay, and mixtures thereof. Other suitable hydrotreating catalysts are, for example, zeolites containing one or more metals. More than one of the aforementioned hydrotreating catalysts can be used together in the second hydrotreating unit HU2.

[0096] The height and diameter of the at least one catalyst bed are selected based on reaction kinetics, optimal liquid / gas flow patterns, and pressure drop. The at least one catalyst bed may consist of one or more layers of different solid absorbent materials, and / or one or more hydrogenation catalysts. The catalyst layers in the at least one catalyst bed may differ from each other in terms of particle size, shape, activity, or active sites. When using more than one catalyst bed, inert particles may be used above and below each bed to improve fluid distribution.

[0097] In the context of this invention, the catalyst for the second hydrogenation unit HU2 is preferably in the form of an extrusion, granules, rings, spherical particles or spheres, more preferably earth-shaped particles or extrusions.

[0098] In the case where the at least one hydrogenation reactor (vessel) in the second hydrogenation treatment unit HU2 has at least two stages, the catalyst preferably has different particle sizes in the at least two stages and / or optionally different shapes in the at least two stages.

[0099] Particle size here refers to particle size distribution, which is measured, for example, by sieving, laser diffraction, or other methods known in the art. Catalysts with desired particle size and optionally desired shape can be manufactured and used.

[0100] Hydrogenation is an exothermic reaction and therefore each stage of the reaction can be optionally cooled.

[0101] The second hydrotreating unit HU2 can operate under various process conditions. For example, the stream S4 containing valuable components is preferably contacted with the hydrotreating catalyst at a temperature preferably from about 200°C to about 400°C, more preferably from about 240°C to about 380°C, and most preferably from about 260°C to about 360°C in the presence of a gas stream S4' containing hydrogen and / or an optional internal recirculated gas stream S6''. Optionally, the gas stream S4' further comprises at least a portion of the stream S2'. The presence of the gas stream S4' is preferred to balance the amount of hydrogen consumed or otherwise lost in the second hydrotreating unit HU2. The aspect of the invention further comprising the optional internal recirculated gas stream S6'' is... Figure 3 As shown in the image.

[0102] The temperature in the second hydrogenation treatment unit HU2 can be obtained by using a preheated stream S4 containing valuable components and / or by using at least one heat exchanger to thermally integrate the stream S4 containing valuable components with the purified stream S6 containing valuable components.

[0103] The pressure during hydrogenation in the second hydrogenation unit HU2 is preferably in the range of about 1 bar to about 200 bar, more preferably about 10 bar to about 150 bar, and most preferably 20 bar to 60 bar.

[0104] The weight time space velocity (WHSV) of the stream S4 containing valuable components is preferably in the range of about 0.1 t / (m²). 3 Kat. •h) to approximately 5 t / (m 3 Kat. •h), more preferably about 0.5 t / (m 3 Kat. •h) to approximately 1.0 t / (m 3 Kat. •h).

[0105] In another aspect of the invention, the second hydrogenation treatment unit HU2 operates with the optional recirculated gas stream S6'' added. This means that hydrogen not consumed by the hydrogenation reaction within the second hydrogenation treatment unit HU2 is separated from streams S6 and S6', and then fed back into the second hydrogenation treatment unit HU2 as recirculated gas stream S6''. The remaining non-hydrogen portion of the exhaust gas stream S2'' and the volatile compounds formed by the hydrogenation reaction with stream S6 leave the second hydrogenation treatment unit HU2 as stream S6''. This aspect... Figure 3 As shown in the image.

[0106] The optional addition of recirculating gas stream S6'', as described above, also benefits the evaporation of stream S4 and its retention in the gas phase. Furthermore, the optional recirculating gas stream S6'' dilutes stream S4. This limits the adiabatic temperature rise caused by the hydrogenation reaction and achieves a high H2 partial pressure, which is beneficial for the hydrogenation activity of the catalyst.

[0107] The ratio “recirculated gas stream S6´´ : stream S4 containing valuable products” is preferably at about 300 Nm 3 / t to approximately 2000 Nm 3 / t, more preferably 500 Nm 3 / t to approximately 800 Nm 3 Between / t.

[0108] More preferably, the stream S6 or a portion thereof is not recycled (re-inserted) into the first hydrogenation treatment unit HU1.

[0109] There is no need to recycle a portion of stream S6 into the first hydrotreating unit HU1 because stream S4 is sufficiently stable relative to undesirable polymerization, and therefore, stream S4 can be vaporized and heated for insertion into the second hydrotreating unit HU2. This enables the establishment of the first hydrotreating unit HU1 (including optional liquid recirculated stream S3') and the second hydrotreating unit HU2 (including recirculated gas) for "one-pass capacity," meaning that liquid stream S1 (and its stream produced by conversion in a separate process unit) passes through the first hydrotreating unit HU1 only once (it exits as stream S3), the distillation unit DU (then enters stream S5 into HU2), and then exits the second hydrotreating unit HU2 as stream S6 (converted).

[0110] Next, in step (vi) of the method according to the invention, the purified stream S6 containing valuable components is separated in at least one aromatic hydrocarbon extraction unit AEU into a benzene-rich stream S7', a toluene-rich stream S7'', a C8 aromatic hydrocarbon-rich stream S7'' (ethylbenzene, 1,2-xylene, 1,3-xylene, 1,4-xylene)-rich stream S7'', and a stream S8 depleted of desired C6-C8 aromatic hydrocarbons.

[0111] The at least one aromatic hydrocarbon extraction unit AEU is downstream of and fluidly connected to the second hydrogenation treatment unit HU2, thereby enabling a stream S6 containing valuable components to flow from the outlet of the second hydrogenation treatment unit HU2 into the at least one aromatic hydrocarbon extraction unit AEU.

[0112] The at least one aromatic hydrocarbon extraction unit AEU can be any unit operation suitable for separating a stream S6 containing valuable components into a benzene-rich stream S7', a toluene-rich stream S7'', and a C8 aromatic hydrocarbon-rich stream S7''. For example, the at least one aromatic hydrocarbon extraction unit AEU can include at least one selective adsorption unit operation, at least one selective absorption unit operation, at least one extractive distillation unit operation, at least one solvent extraction followed by distillation, and combinations thereof.

[0113] Suitable aromatic hydrocarbon extraction units (AEUs) are commercially available, such as Uhde's Morphylane® extractive distillation process. For example, the S6 stream is first split into C... 7- Classification and C 8+ Grade division. Next, C... 7- The fractions are sent to the extractive distillation stage, where the benzene-containing stream S7' and the toluene-containing stream S7'' are mixed with C from stream S6. 7- - Separation of non-aromatic compounds. The C from stream S6... 8+ The fraction is fed directly to the 1,4-xylene circuit without extracting xylene and ethylbenzene.

[0114] Stream S7' preferably contains at least 90 wt.% benzene, more preferably at least 95 wt.% benzene, and most preferably at least 99 wt.% benzene.

[0115] Stream S7'' preferably contains at least 90 wt.% toluene, more preferably at least 95 wt.% toluene, and most preferably at least 99 wt.% toluene.

[0116] Flow S7''' preferably contains at least 90 wt.-% xylene isomers and about 10 wt.-% non-aromatic C 8+ The components, more preferably at least 93 wt.% of xylene isomers and about 2.5 wt.% of non-aromatic C 8+ Components.

[0117] Stream S8 is suitable as a feedstock for cracking processes such as (fluid) catalytic cracking, thermal cracking, and steam cracking. The main reaction products from such cracking processes include ethylene, propylene, butene isomers, butadiene, and pyrolysis gasoline. At least a portion of the pyrolysis gasoline can be used as a co-feedstock in stream S1, together with plastic pyrolysis oil obtained from the pyrolysis of plastic waste. This pyrolysis gasoline contains C6-C8 aromatic hydrocarbons.

[0118] Optionally, the method according to the invention further includes step (vii):

[0119] Stream S7´´ and / or stream S7´´´ undergoes a hydroalkylation unit in at least one optional hydroalkylation unit HAU. In this optional step (vii), toluene and / or xylene isomers and / or ethylbenzene are converted to benzene. Therefore, the benzene yield can be increased by the optional step (vii) in the method according to the invention.

[0120] Hydroalkylation of alkyl-substituted benzene derivatives to benzene and the corresponding hydroalkylation unit HAU are known in the art and described, for example, in HO Folkins' Ullmann's Encyclopedia of Industrial Chemistry, Volume 5, Chapter “Benzene”, pp. 246-251, 2012, and Industrielle organische Chemie, 3rd Edition, K. Weissermel, H.-J. Arpe, pp. 351-352, 1988, both of which are incorporated herein by reference.

[0121] The optional hydroalkylation step (vii) can be operated, for example, as a thermal process (e.g., at about 550°C to about 800°C and at a pressure of about 30 bar to about 100 bar) or as a catalytic process (e.g., at a temperature of about 500°C to about 650°C and at a pressure of about 30 bar to about 50 bar in the presence of a catalyst such as Cr2O3 and / or Mo2O3 on a support such as an alumina support, or at a temperature of about 400°C to about 480°C in the presence of a Rh / Al2O3 catalyst).

[0122] The individual units and their interconnections of chemical equipment used to separate C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil. Figure 2 It is shown in the following description:

[0123] A chemical apparatus for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil comprises: at least one first hydrotreating unit HU1, the at least one first hydrotreating unit HU1 having at least one inlet and at least one outlet; optionally downstream of and fluidly connected to the inlet and outlet of the first hydrotreating unit HU1; at least one distillation unit DU downstream of and fluidly connected to the outlet of the first hydrotreating unit HU1, the at least one distillation unit having a bottom outlet BO and a top outlet HO; a second hydrotreating unit HU2 downstream of and fluidly connected to the top outlet HO of the at least one distillation unit DU; and at least one aromatic hydrocarbon extraction unit AEU downstream of and fluidly connected to the second hydrotreating unit HU2.

[0124] Liquid stream S1 (containing C6-C8 aromatic hydrocarbons, organic compounds containing at least one heteroatom, and compounds having C-C double bonds and / or C-C triple bonds) of plastic pyrolysis oil or a mixture thereof is converted by stream S2 in the first hydrogenation treatment unit HU1. The remainder of stream S2 leaves the first hydrogenation treatment unit HU1 as stream S2'. Liquid stream S1 is converted into stream S3 in the first hydrogenation treatment unit HU1. Optionally, a portion of stream S3 is recycled as stream S3', which is mixed with stream S1 and inserted into the first hydrogenation treatment unit HU1.

[0125] Stream S3 is separated into streams S4 and S5 in the distillation unit DU.

[0126] Optionally, the gas stream S4' further includes at least a portion of the waste gas stream S2'. The gas stream S4' is required to balance the amount of hydrogen consumed or otherwise lost in the second hydrogenation treatment unit HU2.

[0127] In the second hydrogenation treatment unit HU2, stream S4 is converted into stream S6 together with gas stream S4' and optionally additionally with waste gas stream S2'. In this case, gas stream S4' balances the hydrogen demand of the second hydrogenation treatment unit HU2. The remaining non-hydrogen portion of waste gas stream S2'' and the volatile compounds formed by the hydrogenation reaction with stream S6 leave the second hydrogenation treatment unit HU2 as stream S6'.

[0128] Stream S6 enters the aromatic hydrocarbon extraction unit AEU, where stream S6 is separated into streams S7´, S7´´, S7´´´ and S8.

[0129] The specifications of all units and flows are described above in the "Method" section and are preferably the same in the case of the method according to the invention and the chemical equipment according to the invention.

[0130] Optionally, the chemical apparatus according to the invention further includes a hydroalkylation unit HAU, which is downstream of the aromatic hydrocarbon extraction unit AEU and is fluidly connected to stream S7´´ and / or stream S7´´´.

[0131] The invention is further illustrated by the following set of embodiments and by combinations of embodiments derived from the dependent relationships and reverse references shown. In particular, it should be noted that in each instance in which a series of embodiments is mentioned, for example in the context of the term "method as described in any one of Embodiments 1 to 3," each embodiment in this series is intended to clearly disclose to a person skilled in the art that the wording of the term should be understood by a person skilled in the art to be synonymous with "method as described in any one of Embodiments 1, 2, and 3." Furthermore, it should be clearly noted that the following set of embodiments represents a suitable structural portion of the general description of preferred aspects of the invention and, therefore, appropriately supports the claims of the invention.

[0132] 1. A method for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil, the method comprising the following steps:

[0133] (i) Providing a liquid stream S1 comprising at least one plastic pyrolysis oil, the liquid stream S1 further comprising a C6-C8 aromatic hydrocarbon, an organic compound comprising at least one heteroatom, and a compound having a C-C double bond and / or a C-C triple bond.

[0134] (ii) Provide stream S2, which contains H2.

[0135] (iii) The liquid stream S1 and the liquid stream S2 are fed into the hydrogenation unit HU1, in which at least a portion of the components of the liquid stream S1 reacts with the liquid stream S2 in a hydrogenation reaction to form a liquid stream S3, wherein the liquid stream S3 is depleted relative to the liquid stream S1 of compounds having C-C double bonds and / or C-C triple bonds, and

[0136] Optionally, at least a portion of the liquid recirculation stream S3' is fed into the hydrogenation unit HU1, and the liquid recirculation stream S3' is separated from the liquid stream S3. Preferably, the mass ratio of "liquid recirculation stream S3' : liquid stream S3" preferably ranges from about 1 : 1 to about 30 : 1, more preferably from about 5 : 1 to about 20 : 1, and most preferably from about 10 : 1 to about 15 : 1.

[0137] (iv) At least a portion or the remainder of the liquid stream S3 is subjected to a distillation unit DU, in which at least a portion or the remainder of the stream S3 is separated into a stream S4 containing valuable products and a liquid stream S5, wherein the stream S4 containing valuable products comprises C6-C8 aromatic hydrocarbons and organic compounds containing at least one heteroatom.

[0138] (v) The stream S4 containing the valuable product is subjected to a hydrogenation unit HU2, in which the stream S4 is converted into a stream S6, wherein the stream S6 contains C6-C8 aromatic hydrocarbons and is relatively lean compared to stream S4, containing at least one heteroatom and / or C / C double bond of an organic compound, and

[0139] (vi) Separate C6-C8 aromatic hydrocarbons from stream S6 in the aromatic hydrocarbon extraction unit AEU.

[0140] 2. The method according to Example 1, wherein the at least one plastic pyrolysis oil is produced by pyrolysis of plastic waste.

[0141] 3. The method according to Example 1 or 2, wherein the liquid stream S1 preferably contains at least 15 wt.-% of C6-C8 aromatic hydrocarbons, more preferably at least 50 wt.-% of C6-C8 aromatic hydrocarbons, and most preferably at least 80 wt.-% of C6-C8 aromatic hydrocarbons.

[0142] 4. The method according to any one of Examples 1 to 3, wherein the C6-C8 aromatic hydrocarbon in the liquid stream S1 is selected from the group consisting of: benzene, toluene, 1,2-xylene, 1,3-xylene, 1,4-xylene, ethylbenzene and styrene.

[0143] 5. The method according to any one of Examples 1 to 4, wherein the organic compound containing at least one heteroatom is selected from organic compounds containing at least one of the following heteroatoms: nitrogen, oxygen, sulfur, chlorine, bromine, fluorine, and iodine.

[0144] 6. The method according to any one of Examples 1 to 5, wherein the ratio “H2 in fresh H2 feed stream S2 : chemical H2 consumption caused by hydrogenation reaction in the first hydrogenation treatment unit HU1” preferably ranges from about 1:1 to about 5:1, more preferably from about 1:1 to about 3:1 and most preferably from about 1:1 to about 2:1.

[0145] 7. The method according to any one of Examples 1 to 6, wherein the total pressure at the outlet of the at least one reactor in the first hydrogenation treatment unit HU1 is preferably in the range of about 5 bar (absolute value) to about 60 bar (absolute value), more preferably about 10 bar (absolute value) to about 40 bar (absolute value) and most preferably about 20 bar (absolute value) to about 40 bar (absolute value).

[0146] 8. The method according to any one of Examples 1 to 7, wherein the at least one plastic pyrolysis oil in the liquid stream S1 has a bromine value of about 2 g Br2 / 100 g to about 150 g Br2 / 100 g (determined by ASTM 1159) and / or a C5 hydrocarbon content of about 0.03 wt.-% to about 12.2 wt.-% (determined by ASTM D 5134) and / or a naphthalene content of about 0.5 wt.-% to about 18.4 wt.-% (determined by ASTM D 5134) and / or a styrene content of about 0.02 wt.-% to about 29.5 wt.-% (determined by ASTM D 5134) and / or a toluene content of about 4.3 wt.-% to about 71.5 wt.-% (determined by ASTM D 5134).

[0147] 9. The method according to any one of Examples 1 to 8, wherein the H2 contained in the stream S2 is formed by water electrolysis using electrical energy, which is preferably generated from a renewable source and / or a low-carbon energy source.

[0148] 10. The method according to any one of Examples 1 to 9, wherein the liquid stream S1 and the stream S2 are mixed before being fed into the first hydrogenation treatment unit HU1.

[0149] 11. The method according to any one of Examples 1 to 10, wherein the liquid stream S1 and the stream S2 are respectively fed into the first hydrogenation treatment unit HU1.

[0150] 12. The method according to any one of Examples 1 to 11, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor, preferably at least one three-phase reactor having at least one catalyst bed.

[0151] 13. The method according to any one of Examples 1 to 12, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor having at least one fixed catalyst bed, the at least one fixed bed comprising at least one heterogeneous catalyst.

[0152] 14. The method according to any one of Examples 1 to 13, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor operating in trickle or pulse flow mode.

[0153] 15. The method according to any one of Examples 1 to 14, wherein the first hydrogenation treatment unit HU1 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst comprising at least one catalytically active metal selected from elements of Groups 8 to 12 of the periodic table, more preferably the at least one catalytically active metal selected from the group consisting of or composed of the following: nickel, palladium, platinum, rhodium, and most preferably the catalytically active metal is palladium.

[0154] 16. The method according to any one of Examples 1 to 15, wherein the first hydrogenation treatment unit HU1 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst further comprising a support, preferably an inorganic support, more preferably a support selected from the group consisting of or composed of: silica, alumina, silica-alumina, magnesium oxide, clay, carbon and mixtures thereof.

[0155] 17. The method according to any one of Examples 1 to 16, wherein the first hydrogenation treatment unit HU1 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst comprising at least one catalytically active metal selected from the group consisting of or composed of the following: nickel, palladium, platinum and rhodium, and further comprising a support selected from the group consisting of or composed of the following: silica, alumina, silica-alumina, magnesium oxide, clay, carbon and mixtures thereof.

[0156] 18. The method according to any one of Examples 1 to 17, wherein the first hydrogenation treatment unit HU1 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst comprising palladium, more preferably in an amount of palladium calculated as elemental palladium in the range of about 0.01 wt.-% to about 5 wt.-%, more preferably about 0.1 wt.-% to about 1 wt.-%, and most preferably 0.15 wt.-% to 0.8 wt.-%.

[0157] 19. The method according to any one of Examples 1 to 18, wherein the temperature of the hydrogenation reaction in the first hydrogenation treatment unit HU1 is preferably in the range of about 40°C to about 250°C, more preferably about 60°C to about 200°C, and most preferably about 80°C to about 120°C.

[0158] 20. The method according to any one of Examples 1 to 19, wherein the compound having C-C double bonds and / or C-C triple bonds and / or styrene contained in the liquid stream S1 is at least 90% depleted in the first hydrogenation treatment unit HU1.

[0159] 21. The method according to any one of Examples 1 to 20, wherein at least a portion of the recirculated stream S3' is fed together with the liquid stream S1 and the stream S2 into the first hydrogenation treatment unit HU1.

[0160] 22. The method according to any one of Examples 1 to 21, wherein the distillation unit DU preferably comprises a distillation column.

[0161] 23. The method according to any one of Examples 1 to 22, wherein distillation in the distillation unit DU is carried out at a temperature ranging from about 0°C to about 600°C, more preferably from about 20°C to about 400°C, and most preferably from about 80°C to about 250°C, and at a pressure ranging from about 0.001 bar to about 4 bar (absolute value), more preferably from about 0.001 bar to about 2.0 bar (absolute value), and most preferably from about 0.9 bar to about 1.8 bar (absolute value), wherein the temperature is adjusted accordingly if the pressure is ≠ 1.013 bar.

[0162] 24. The method according to any one of Examples 1 to 23, wherein the stream S4 containing the valuable product comprises about 60% to about 99% of the C6-C8 aromatic hydrocarbons contained in the liquid stream S1.

[0163] 25. The method according to any one of Examples 1 to 24, wherein the stream S5 is then converted into syngas in at least one gasifier and / or partial oxidation reaction unit.

[0164] 26. The method according to any one of Examples 1 to 25, wherein the second hydrogenation treatment unit HU2 comprises at least one fixed-bed reactor.

[0165] 28. The method according to any one of Examples 1 to 26, wherein the second hydrogenation treatment unit HU2 comprises at least one heterogeneous catalyst.

[0166] 29. The method according to any one of Examples 1 to 28, wherein the second hydrogenation treatment unit HU2 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst comprising or consisting of at least one of the following: Co-Mo catalyst, Ni-Mo catalyst, Ni-W catalyst, Co-W catalyst and Mo catalyst, and preferably further comprising at least a catalyst support material selected from the group comprising or consisting of the following: alumina, silica, magnesium oxide, zirconium oxide, titanium dioxide, zeolite material, silica-alumina phosphate (SAPO) material, zinc oxide, sodium oxide, mixed silica-alumina, zeolite and calcium oxide, more preferably alumina.

[0167] 30. The method according to any one of Examples 1 to 29, wherein the temperature of the hydrogenation reaction in the second hydrogenation treatment unit HU2 is preferably in the range of about 200°C to about 400°C, more preferably about 240°C to about 380°C, and most preferably about 260°C to about 360°C.

[0168] 31. The method according to any one of Examples 1 to 30, wherein the pressure of the hydrogenation reaction in the second hydrogenation treatment unit HU2 is preferably in the range of about 1 bar to about 200 bar, more preferably about 10 bar to about 150 bar, and most preferably about 20 bar to about 60 bar.

[0169] 32. The method according to any one of Examples 1 to 31, wherein the weight time space velocity (WHSV) of the stream S4 containing the valuable component is preferably in the range of about 0.1 t / (m²). 3 Kat. •h) to approximately 5 t / (m 3 Kat. •h), more preferably about 0.5 t / (m 3 Kat. •h) to approximately 1.0 t / (m 3 Kat. •h).

[0170] 33. The method according to any one of Examples 1 to 32, wherein the ratio “recirculated gas stream S6´´ : stream S4 containing valuable products” is preferably at about 300 Nm 3 / t to approximately 2000 Nm 3 / t, more preferably 500 Nm 3 / t to approximately 800 Nm 3 Between / t.

[0171] 34. The method according to any one of Examples 1 to 33, wherein the organic compound containing at least one heteroatom in stream S3 is at least 90%, more preferably at least 99%, depleted in the second hydrogenation treatment unit HU2.

[0172] 35. The method according to any one of Examples 1 to 34, wherein at least one of NH4F, NH4Cl, NH4Br, NH4I and NH4SH is formed in the second hydrogenation treatment unit HU2, and wherein at least one of NH4Cl, NH4F, NH4Br, and NH4I is quantitatively removed from the second hydrogenation treatment unit HU2 with water and / or wherein NH4SH is partially removed from the second hydrogenation treatment unit HU2 with water.

[0173] 36. The method according to any one of Examples 1 to 35, wherein C6-C8 aromatic hydrocarbons are separated from stream S6 by extractive distillation in at least one aromatic hydrocarbon extraction unit AEU.

[0174] 37. The method according to any one of Examples 1 to 36, wherein, by separating C6-C8 aromatic hydrocarbons from stream S6 in the at least one aromatic hydrocarbon extraction unit AEU, a stream S7' containing at least 90 wt.-% benzene, a stream S7'' containing at least 90 wt.-% toluene, a stream S7''' containing at least 90 wt.-% C8 aromatic hydrocarbons selected from the group consisting of 1,2-xylene, 1,3-xylene, 1,4-xylene and ethylbenzene, and a stream S8 leaning from C6-C8 aromatic hydrocarbons are obtained.

[0175] 38. The method according to Example 37, wherein the stream S8 is further subjected to a cracking process selected from the group consisting of catalytic cracking, thermal cracking and steam cracking.

[0176] 39. A chemical apparatus for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil, the apparatus comprising...

[0177] (i) at least one first hydrogenation processing unit HU1, the at least one first hydrogenation processing unit HU1 comprising at least one inlet and at least one outlet.

[0178] (ii) Optionally, a recirculation unit is located downstream of and fluidly connected to the inlet and outlet of the first hydrogenation treatment unit HU1.

[0179] (iii) A distillation unit DU, which is downstream of and fluidly connected to the outlet of the first hydrogenation treatment unit HU1, the at least one distillation unit having a bottom outlet BO and a top outlet HO.

[0180] (iv) A second hydrogenation treatment unit HU2, which is downstream of and fluidly connected to the top outlet HO of the at least one distillation unit DU.

[0181] (v) At least one aromatic hydrocarbon extraction unit AEU, which is downstream of and fluidly connected to the second hydrogenation treatment unit HU2.

[0182] 40. The chemical equipment according to Example 39, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor, preferably wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor having at least one fixed catalyst bed.

[0183] 41. The chemical equipment according to any one of Examples 39 or 40, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor having at least one fixed catalyst bed, the at least one fixed bed comprising at least one heterogeneous catalyst.

[0184] 42. The chemical equipment according to any one of Examples 39 to 41, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor having at least one fixed catalyst bed, the at least one fixed bed comprising at least one catalyst used in at least one stage of the at least one three-phase reactor.

[0185] 43. The chemical equipment according to any one of Examples 39 to 42, wherein the first hydrogenation treatment unit HU1 comprises at least one three-phase reactor operating in trickle or pulse flow mode.

[0186] 44. The chemical equipment according to any one of Examples 39 to 43, wherein the first hydrogenation treatment unit HU1 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst comprising: at least one element selected from Groups 8 to 12 of the periodic table, more preferably selected from the group consisting of: nickel, palladium, platinum, rhodium, and most preferably palladium; and at least one support, the support preferably being an inorganic support, more preferably selected from the group consisting of: silica, alumina, silica-alumina, silica-alumina phosphate, magnesium oxide, clay, carbon, and mixtures thereof.

[0187] 45. The chemical equipment according to any one of Examples 39 to 44, wherein the distillation unit DU preferably includes a distillation column.

[0188] 45. The chemical equipment according to any one of Examples 39 to 44, wherein the second hydrogenation treatment unit HU2 comprises at least one fixed-bed reactor.

[0189] 46. ​​The chemical equipment according to any one of Examples 39 to 45, wherein the second hydrogenation treatment unit HU2 comprises at least one heterogeneous catalyst.

[0190] 47. The chemical equipment according to any one of Examples 39 to 46, wherein the second hydrogenation treatment unit HU2 comprises at least one heterogeneous catalyst, the at least one heterogeneous catalyst comprising at least one of Co-Mo catalyst, Ni-Mo catalyst, Ni-W catalyst, Co-W catalyst and Mo catalyst, and preferably further comprising at least one catalyst support material selected from the group consisting of: alumina, silica, magnesium oxide, zirconium oxide, titanium dioxide, zeolite material, silica-alumina phosphate (SAPO) material, zinc oxide, sodium oxide, mixed silica-alumina, zeolite and calcium oxide, more preferably alumina.

[0191] 48. The chemical apparatus according to any one of Examples 39 to 47, wherein the at least one aromatic hydrocarbon extraction unit (AEU) comprises at least one extractive distillation unit.

[0192] 49. Use of the chemical equipment according to any one of Examples 39 to 48 for the method according to any one of Examples 1 to 38.

[0193] 50. A computer program comprising instructions which, when executed by a chemical apparatus according to any one of embodiments 39 to 48, cause the system to perform the method according to any one of embodiments 1 to 38.

[0194] It should be clearly noted that the above set of embodiments represents appropriate structural portions of a general description of preferred aspects of the invention, and therefore appropriately supports but does not represent the claims of the invention.

[0195] Stream S5 can be further used as a feedstock for a partial oxidation process and thus converted into a syngas stream containing H2, CO and CO2.

[0196] Stream S8 can be further used as feedstock for a cracking process, preferably a steam cracking process, and thus converted into a stream containing at least one olefin and / or at least one C6-C8 aromatic hydrocarbon, wherein the at least one olefin is preferably selected from the group consisting of ethylene, propylene, n-butene, 2-butene and butadiene.

[0197] The C6-C8 aromatic hydrocarbons contained in the corresponding streams S7´, S7´´ and S7´´´ can be further used as feedstocks in downstream processes.

[0198] The present invention further relates to a method, according to the method described herein, comprising the following additional steps:

[0199] - C6-C8 aromatic hydrocarbons that are available or obtainable by the methods described herein; and / or syngas that are available or obtainable by the methods described herein; and / or chemical materials that are available or obtainable by the methods described herein, preferably by subjecting stream S8 to a cracking process to convert the chemical materials that are available or obtainable by the methods described herein into monomers, polymers or polymer products.

[0200] The conversion steps to obtain chemical materials, monomers, polymers, or polymer products may include one or more synthetic steps and can be carried out by conventional synthesis and techniques well known to those skilled in the art. Those skilled in the art, independent of those evaluating the novelty and inventive step of the independent claim, preferably come from one or more technical fields of pyrolysis, gasification, re-monomerization, depolymerization, synthesis, production of monomers, polymers, and polymer compounds, and / or their further processing (e.g., extrusion, injection molding). Examples of the conversion steps are described in "Industrial Organic Chemistry", Volume 3, Wiley-VCH, 1997, ISBN: 978-3-527-28838-0; "Kunststoffhandbuch", Volume 11 of 17 sub-volumes, Carl Hanser Verlag; especially Volume 6, "Polyamide", 1st edition, 1966; Volume 7, "Polyurethane", 3rd edition, 1993; and Volume 8, "Polyester", 1st edition, 1973; "Industrial Organic Chemistry", Volume 3, Wiley-VCH, 1997, ISBN: 978-3-527-28838-0; "Injection Molding Reference" Injection Molding Reference Guide, 4th Edition, CreateSpace Independent Publishing Platform, 2011, ISBN: 978-1466407824; EP0989146 (A1); EP1460094 (A1); WO 2006034800 (A1); EP1529792 (A1); WO 2006042674 (A1); EP0364854 (A2); US5506275 (A); EP0897402 (A1); WO 2015082316 (A1); WO 2021021855 (A1); WO2021126938 (A1); WO 2021021902 (A1); WO 2021092311 (A1); WO 2008155271 (A1); WO2013139827 (A1), each of which is incorporated herein by reference.

[0201] In a preferred embodiment, the monomer is a diol or polyol, preferably butanediol; an aldehyde, preferably formaldehyde; a diisocyanate or polyisocyanate, preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylene diisocyanate (HDI) or isophorone diisocyanate (IPDI); an amide, preferably caprolactam; an olefin, preferably styrene, ethylene and norbornene; an alkyne; a (di) ester, preferably methyl methacrylate; a monoacid or diacid, preferably adipic acid or terephthalic acid; a diamine, preferably hexamethylenediamine or nonadiamine; or a sulfone, preferably 4,4'-dichlorodiphenyl sulfone.

[0202] In a preferred embodiment, the polymer and / or the polymer product comprises polyamide (PA), preferably PA 6 or PA 66; a polyisocyanate addition polymer, preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), polyacrylonitrile butadiene styrene (ABS), polystyrene acrylonitrile (SAN), polyacrylate styrene acrylonitrile polyacrylate (ASA), polytetrafluoroethylene (PTFE), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis-1,4-isoprene), poly(trans-1,4-isoprene) Poly(pentadiene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate (PBAT), polyester (PES), polyethersulfone (PESU), polyhydroxyalkanoate (PHA), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyetheretherketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymers or mixtures thereof.

[0203] In a preferred embodiment, the polymer and / or polymer product is then converted into the following or a portion thereof:

[0204] - Automotive parts, preferably cylinder head covers, engine hoods, turbocharger housings, turbocharger baffles, intake pipes, intake manifolds, connectors, gears, fan wheels, coolant tanks, housings, heat exchanger housing parts, coolant coolers, turbocharger coolers, thermostats, water pumps, radiators, fasteners, battery system parts for electric vehicles, dashboards, steering column switches, seats, headrests, center consoles, transmission components, door modules, A, B, C, or D pillar covers, spoilers, door handles, exterior mirrors, windshield wipers, windshield wiper protection housings, decorative grilles, cover strips, roof rails, window frames, sunroof frames, antenna panels, headlights and taillights, engine hoods, cylinder head covers, intake manifolds, airbags, cushioning pads or coatings;

[0205] - Fabrics, preferably shirts, trousers, sweaters, boots, shoes, shoe soles, bodysuits or jackets;

[0206] - Electrical components, preferably electrical or electronic passive or active components, circuit boards, printed circuit boards, housing components, foil, wires, switches, plugs, sockets, distributors, relays, resistors, capacitors, inductors, spools, lamps, diodes, LEDs, transistors, connectors, voltage regulators, integrated circuits (ICs), processors, controllers, memory, sensors, microswitches, micro buttons, semiconductors, reflector housings for light-emitting diodes (LEDs), fasteners, gaskets, bolts, strips, slide-in guides, screws, nuts, membrane hinges, spring hooks (clamp-in) or spring tongues;

[0207] - Consumer goods, agricultural products, or pharmaceutical products, preferably tennis strings, climbing ropes, bristles, brushes, artificial turf, 3D printed filaments, lawnmowers, zippers, hook and loop fasteners, paper machine fabrics, extrusion coatings, fishing lines, fishing nets, offshore lines and ropes, vials, syringes, ampoules, bottles, sliding elements, spindle nuts, chain conveyors, sliding bearings, rollers, wheels, gears, ring gears, screws and spring dampers, hoses, pipes, cable sheaths, sockets, switches, cable ties, fan wheels, carpets, cosmetic boxes or bottles, mattresses, cushioning pads, insulating materials, detergents, dishwasher detergent blocks or powders, shampoos, shower gels, bath gels, soaps, fertilizers, fungicides, or pest control agents;

[0208] - For packaging in the food industry, single-layer or multi-layer blown film, cast film (single-layer or multi-layer), biaxial stretch film, or laminated film are preferred; or

[0209] - Structural components, preferably rotor blades, insulating materials, frames, housings, walls, coatings, or partition walls.

[0210] In a preferred embodiment, the content of liquid stream S1 in the monomer, polymer, or polymer product is 1 wt% or more, preferably 2 wt% or more, more preferably 5 wt% or more, more preferably 15 wt% or more, more preferably 30 wt% or more, more preferably 40 wt% or more, more preferably 60 wt% or more, more preferably 80 wt% or more, more preferably 90 wt% or more, more preferably 95 wt% or more; and / or

[0211] The content of liquid stream S1 in the monomer, polymer, or polymer product is 100 wt% or less, preferably 95 wt% or less, more preferably 90 wt% or less, more preferably 50 wt% or less, more preferably 25 wt% or less, more preferably 10 wt% or less; and preferably the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably according to the International Sustainability and Carbon Certification (ISCC) standard.

[0212] The present invention will be further explained through the following non-limiting examples. Example

[0213] Using ASPEN Plus TM The V11 simulation software is combined with a kinetic model to simulate a method for separating C6-C8 aromatic hydrocarbons from plastic pyrolysis oil (comparative examples and the method according to the invention) to calculate the conversion rates in the first hydrotreating unit HU1 and the second hydrotreating unit HU2.

[0214] Comparison Examples

[0215] A comparative example is a method and chemical apparatus for producing C6-C8 aromatic hydrocarbons from a liquid stream S1 containing plastic pyrolysis oil obtained from the pyrolysis of plastic waste as taught in AU 2021 / 222788 A1, and in... Figure 1 It is shown schematically in the diagram.

[0216] The process conditions for the first hydrogenation treatment unit HU1 are summarized in Table 1:

[0217]

[0218]

[0219] The composition of liquid stream S1 in hydrotreating unit HU1 is described in Table 2, wherein the diene component concentration is 0.8 wt.-% and the olefin component concentration is 3.23 wt.%. The total content of C6-C8 aromatic compounds is 73.13 wt.-%. The composition of liquid stream S1 is the same as that used in the following examples according to the invention. Liquid stream S1 is treated in hydrotreating unit HU1 under the conditions described in Table 1.

[0220] The catalyst in the hydrotreating unit HU1 is a Ni-Mo catalyst on an alumina support taught in AU 2021 / 222788 A1.

[0221] The pressure at the reactor outlet of the first hydrogenation unit HU1 is 64 bar (absolute value), and the reactor temperature is increased from 119°C (reactor inlet temperature) to 150°C (reactor outlet temperature) through adiabatic temperature rise. Under these conditions, typical trickle bed flow of the liquid phase over the (solid) catalyst occurs, which is desirable.

[0222] From the hydrogenation treatment unit HU2 ( Figure 1 The ratio of "liquid feed S1 : liquid recirculation flow S3'" is 1 : 1. Therefore, the concentration of diene components in the reactor inlet flow S1', having 0.4 wt.% is 5.7 times the concentration of diene components in the example according to the invention (see below). The much higher temperature increase (from reactor inlet to reactor outlet of the first hydrogenation treatment unit HU1) compared to 5°C in the example according to the invention (see below), along with the much higher diene component concentration, leads to higher polymer formation during treatment and thus promotes blockage, both of which are undesirable.

[0223] The WHSV (weight hourly space velocity) of liquid flow S1 is 0.5 t / (m²). 3 Kat. h). The chemical hydrogen consumption in the hydrogenation unit HU1 is 23 Nm. 3 / t. The molar ratio of "feed to hydrotreating unit HU1 containing H2 stream S2 : chemical hydrogen consumption" is 1.08 : 1. A small excess of hydrogen ensures sufficient catalyst activity to achieve 99% conversion of diene components and 68% conversion of olefin components (stream S3). Under these operating conditions and with the catalyst used (Ni-Mo catalyst on alumina support), no hydrogenation of aromatic components will occur. The reactor products of hydrotreating unit HU1 ( Figure 1The feed (S3) is directly fed into the hydrotreating unit HU2.

[0224] The process conditions in the second hydrogenation unit HU2 are summarized in Table 3:

[0225]

[0226] Table 3 shows the process conditions for the hydrotreating unit HU2. The pressure at the reactor outlet is 63 bar (absolute). The ratio of "HU2 internal recirculated gas S4'' : feed stream S3" is 392 Nm. 3 / t, and the reactor inlet temperature of the second hydrotreating unit HU2 is 342°C. Under these conditions, the feed stream S3 of the hydrotreating unit HU2 is completely evaporated.

[0227] Due to the feed stream S3 of the hydrotreating unit HU2 < A low diene content of 0.01 wt.% does not result in undesirable polymerization and scaling during complete evaporation. Through the exothermic hydrogenation reaction mentioned above, the reactor temperature is increased from an inlet temperature of 342°C to an outlet temperature of 355°C. The temperature increase is 13°C because 69% of the olefins have already been hydrogenated in the hydrogenation treatment unit HU1.

[0228] To limit undesirable hydrogenation of aromatic rings, this low exothermic temperature increase of 13°C is beneficial. A hydrogen partial pressure of 39 bar (absolute value) in the reactor is sufficient to ensure adequate hydrogenation activity while avoiding undesirable aromatic ring hydrogenation. The catalyst in the hydrotreating unit HU2 is a standard Co-Mo catalyst on an alumina support, which exhibits sufficient activity for diene and olefin hydrogenation, desulfurization, denitrification, and dehalogenation, as well as very low aromatic ring hydrogenation activity, but requires a higher temperature than the Co-Mo catalyst on an alumina support described in the example below according to the invention. The loss of aromatic components through aromatic ring hydrogenation is <0.5%. The WHSV of the feed stream S3 is 0.7 t / (m³). 3 Kat. h).

[0229] The cooled condensate reaction product S4 leaving the second hydrotreating unit HU2 is fed back to the hydrotreating unit HU1 at a 1:1 ratio along with the liquid feed stream S1 to dilute the liquid feed stream S1 before it enters the first hydrotreating unit HU1. The necessity and effect of dilution in the hydrotreating unit HU1 have been described above.

[0230] The next step is distillation in the distillation unit DU to remove unwanted high-boiling components before the aromatic hydrocarbon extraction unit AEU. High-boiling components are undesirable in the aromatic hydrocarbon extraction unit AEU because they accumulate in the solvent and contaminate it. Therefore, the efficiency of aromatic hydrocarbon extraction in the aromatic hydrocarbon extraction unit AEU will be affected.

[0231] The distillation results in distillation unit DU are shown in Table 4.

[0232]

[0233] In distillation unit DU, the light boiling fraction, containing the majority of C6-C8 aromatic components, enters the overhead distillate. This constitutes 78 wt.-% of the feed stream S4 to distillation unit DU, thus increasing the C6-C8 aromatic component content from 69.5 wt.-% to 83.0 wt.-%. The high-boiling components are separated by the bottom stream S5. The valuable product overhead distillate S4 is 78% of the feed stream S3 to distillation unit DU and contains 93 wt.-% C6-C8 aromatic components.

[0234] The feed stream S6 from the head section of the distillation unit DU is then fed into the aromatic hydrocarbon extraction unit AEU. Here, pure benzene (> 99 wt.-%), pure toluene (> 99 wt.-%), and the xylene / ethylbenzene mixture (> 93 wt.-%) are separated by an extractive distillation process. The remaining stream S8 is lean for C6-C8 aromatic components and contains paraffinic components, cycloalkanes, and C8+ aromatic hydrocarbons.

[0235] Example (of this invention)

[0236] In this example, according to Figure 3 The schematic diagram in the figure simulates the method according to the present invention.

[0237] Table 5. Process conditions in the first hydrogenation treatment unit HU1:

[0238]

[0239]

[0240] The composition of the liquid stream S1 fed into the first hydrotreating unit HU1 is described in Table 6, wherein the diene component concentration is 0.8 wt.-% and the olefin component concentration is 3.23 wt.%. The total content of C6-C8 aromatic compounds is 73.13 wt.-%. Liquid stream S1 is treated in the first hydrotreating unit HU1 under the conditions described in Table 5. The catalyst in the first hydrotreating unit HU1 is a palladium catalyst contained on an alumina support, which allows for very mild reaction conditions (e.g., lower temperatures). The pressure at the reactor outlet in the first hydrotreating unit HU1 is 30 bar (absolute), and the reactor temperature is increased from a reactor inlet temperature of 80°C to a reactor outlet temperature of 85°C by adiabatic temperature increase. Under these conditions, typical trickle bed flow of the liquid phase over the catalyst occurs. The ratio "liquid feed S1 : liquid recirculation flow S3'" results in a very low diene concentration of 0.07 wt.% and an olefin content of 0.97 wt.% in the reactor inlet flow S1'. The low temperature and mild temperature increase of only 6°C, combined with the high pressure and low diene concentration, ensure that undesirable polymer formation and fouling are avoided during treatment.

[0241] The WHSV (weight hourly space velocity) of liquid flow S1 is 0.5 t / (m²). 3 Kat. h). The chemical hydrogen consumption in the first hydrogenation unit HU1 is 28 Nm. 3 The molar ratio of "hydrogen-containing stream S2 fed to the first hydrogenation unit HU1 : chemical hydrogen consumption" is 1.2 : 1. A small excess of hydrogen ensures sufficient catalyst activity to achieve 99% conversion of diene components and 76% conversion of olefin components (stream S3). Under these operating conditions, no hydrogenation of aromatic components will occur. Stream S3 leaving the first hydrogenation unit HU1 is sufficiently stable and no undesirable scaling caused by polymerization occurs in the distillation unit DU.

[0242] The distillation results in distillation unit DU are shown in Table 7:

[0243]

[0244] For liquid stream S1, it is necessary to separate high-boiling-point substances from stream S3 to ensure that stream S3 is completely evaporated in the second hydrogenation treatment unit HU2.

[0245] In distillation unit DU, the light boiling fraction, containing the majority of C6-C8 aromatics, enters the overhead distillate. This constitutes 78 wt.-% of the total feed to distillation unit DU stream S4. The C6-C8 aromatic content increases from 69.0 wt.-% to 82.5 wt.%. High-boiling components are separated by the bottom stream S5. The valuable product overhead distillate S4 is 78 wt.-% of the feed stream S3 from distillation unit DU and contains 93 wt.-% C6-C8 aromatics.

[0246] The valuable overhead distillate stream S4 from distillation unit DU is further processed in the second hydrotreating unit HU2. Here, the remaining trace amounts of dienes and alkenes are hydrogenated in the gas phase to the corresponding saturated hydrocarbons. Sulfur-containing components are hydrogenated to the corresponding saturated hydrocarbons and H₂S. The sulfur content in the hydrotreating product stream S6 is < 0.5 wt.-ppm. Nitrogen-containing components are hydrogenated to the corresponding saturated hydrocarbons and NH₃. The nitrogen content in the hydrotreating product stream S6 is < 10 wt.-ppm. Halogen-containing components (such as chlorine-containing components) are hydrogenated to the corresponding saturated hydrocarbons and hydrohalic acids (such as HCl). The halogen / chlorine content in the hydrotreating product stream S6 is < 1 wt.-ppm.

[0247] The process conditions for the second hydrogenation unit HU2 are shown in Table 8:

[0248]

[0249] Table 8 shows the process conditions for the second hydrogenation unit HU2. The pressure at the reactor outlet is 51 bar (absolute value). The ratio of "recirculated gas flow S6'' : feed flow S4" is 577 Nm. 3 / t, and the reactor inlet temperature is 267°C. Under these conditions, the inlet stream S4 of the second hydrogenation treatment unit HU2 is completely evaporated. Due to the feed stream S4 < A low content of diene components (0.01 wt.%) prevents unwanted polymerization and scaling within the second hydrotreating unit HU2. Through the exothermic hydrogenation reaction within the second hydrotreating unit HU2 mentioned above, the reactor temperature is increased from an inlet temperature of 267°C to an outlet temperature of 281°C. This temperature increase is advantageously limited to a lower 14°C because 76% of the olefins have already been hydrogenated in the first hydrotreating unit HU1. This low exothermic temperature increase within the second hydrotreating unit HU2 is beneficial in limiting the unwanted hydrogenation of C6-C8 aromatics. The hydrogen partial pressure of 36 bar in the reactor of the second hydrotreating unit HU2 is suitable for ensuring sufficient hydrogenation activity while avoiding the unwanted hydrogenation of C6-C8 aromatics.

[0250] The catalyst in the second hydrotreating unit HU2 is a Co-Mo catalyst on an alumina support, which exhibits sufficient activity for diene and olefin hydrogenation, desulfurization, denitrification, and dehalogenation, as well as the desired very low activity for C6-C8 aromatic hydrocarbon hydrogenation. The loss of aromatic components through aromatic ring hydrogenation is <0.5%. The WHSV of stream S4 is 0.7 t / (m³). 3 Kat. h).

[0251] Stream S6, exiting the second hydrogenation unit HU2, is fed to the aromatics extraction unit AEU, which produces pure benzene (>99 wt.-%), pure toluene (>99 wt.-%), and a xylene / ethylbenzene mixture (>93 wt.-%), which are separated in the aromatics extraction unit AEU by extractive distillation. The remaining stream S8 is lean for C6-C8 aromatics and contains paraffinic components, cycloalkanes, and C8+ aromatics.

Claims

1. A method for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil, the method comprising the following steps: (i) Providing a liquid stream S1 comprising at least one plastic pyrolysis oil, the liquid stream S1 further comprising a C6-C8 aromatic hydrocarbon, an organic compound comprising at least one heteroatom, and a compound having a C-C double bond and / or a C-C triple bond. (ii) Provide stream S2, which contains H2, (iii) The liquid stream S1 and the liquid stream S2 are fed into a hydrogenation unit HU1, in which at least a portion of the components of the liquid stream S1 reacts with the liquid stream S2 in a hydrogenation reaction to form a liquid stream S3, wherein the liquid stream S3 is depleted relative to the liquid stream S1 of compounds having C-C double bonds and / or C-C triple bonds, and Optionally, at least a portion of the liquid recirculation stream S3' is fed into the hydrogenation unit HU1, the liquid recirculation stream S3' being separated from the liquid stream S3, preferably wherein the mass ratio of "liquid recirculation stream S3' : liquid stream S3" preferably ranges from about 1 : 1 to about 30 : 1, more preferably from about 5 : 1 to about 20 : 1, and most preferably from about 10 : 1 to about 15 :

1. (iv) At least a portion or the remainder of the liquid stream S3 is subjected to a distillation unit DU, in which at least a portion or the remainder of the stream S3 is separated into a stream S4 containing valuable products and a liquid stream S5, wherein the stream S4 containing valuable products comprises C6-C8 aromatic hydrocarbons and organic compounds containing at least one heteroatom. (v) The stream S4 containing the valuable product is subjected to a hydrogenation unit HU2, in which the stream S4 is converted into a stream S6, wherein the stream S6 contains C6-C8 aromatic hydrocarbons and is relatively lean compared to stream S4, containing at least one heteroatom and / or C / C double bond of an organic compound, and (vi) Separate C6-C8 aromatic hydrocarbons from stream S6 in the aromatic hydrocarbon extraction unit AEU.

2. The method according to claim 1, wherein, This at least one type of plastic pyrolysis oil is produced by the pyrolysis of plastic waste.

3. The method according to claim 1 or 2, wherein, The liquid stream S1 preferably contains at least 15 wt.% of C6-C8 aromatic hydrocarbons, more preferably at least 50 wt.% of C6-C8 aromatic hydrocarbons, and most preferably at least 80 wt.% of C6-C8 aromatic hydrocarbons.

4. The method according to any one of claims 1 to 3, wherein, The at least one plastic pyrolysis oil in the liquid stream S1 has a bromine value of about 2 g Br2 / 100 g to about 150 g Br2 / 100 g (as determined by ASTM 1159) and / or a C5 hydrocarbon content of about 0.03 wt.-% to about 12.2 wt.-% (as determined by ASTM D 5134) and / or a naphthalene content of about 0.5 wt.-% to about 18.4 wt.-% (as determined by ASTM D 5134) and / or a styrene content of about 0.02 wt.-% to about 29.5 wt.-% (as determined by ASTM D 5134) and / or a toluene content of about 4.3 wt.-% to about 71.5 wt.-% (as determined by ASTM D 5134).

5. The method according to any one of claims 1 to 4, wherein, The first hydrogenation treatment unit HU1 includes at least one three-phase reactor, preferably at least one three-phase reactor having at least one fixed catalyst bed.

6. The method according to any one of claims 1 to 5, wherein, The first hydrogenation treatment unit HU1 includes at least one heterogeneous catalyst, which includes at least one catalytically active metal selected from elements of groups 8 to 12 of the periodic table. More preferably, the at least one catalytically active metal is selected from the group consisting of nickel, palladium, platinum, and rhodium, and most preferably, the catalytically active metal is palladium.

7. The method according to any one of claims 1 to 6, wherein, The ratio "H2 in the fresh H2 feed stream S2 : chemical H2 consumption caused by the hydrogenation reaction in the first hydrogenation treatment unit HU1" preferably ranges from about 1:1 to about 5:1, more preferably from about 1:1 to about 3:1, and most preferably from about 1:1 to about 2:

1.

8. The method according to any one of claims 1 to 7, wherein, The total pressure at the outlet of the at least one reactor in the first hydrogenation treatment unit HU1 is preferably in the range of about 5 bar (absolute value) to about 60 bar (absolute value), more preferably about 10 bar (absolute value) to about 40 bar (absolute value), and most preferably about 20 bar (absolute value) to about 40 bar (absolute value).

9. The method according to any one of claims 1 to 8, wherein, The mass ratio of "liquid recirculation flow S3' : liquid flow S3" preferably ranges from about 1 : 1 to about 30 : 1, more preferably from about 5 : 1 to about 20 : 1, and most preferably from about 10 : 1 to about 15 :

1.

10. The method according to any one of claims 1 to 9, wherein, The second hydrogenation unit HU2 includes at least one fixed-bed reactor.

11. The method according to any one of claims 1 to 10, wherein, The first hydrogenation treatment unit HU1 contains at least one heterogeneous catalyst, which contains at least one catalytically active metal selected from the group consisting of nickel, palladium, platinum and rhodium.

12. The method according to any one of claims 1 to 11, wherein, The second hydrogenation treatment unit HU2 includes at least one heterogeneous catalyst selected from or consisting of the group consisting of: Co-Mo catalyst, Ni-Mo catalyst, Ni-W catalyst, Co-W catalyst and Mo catalyst.

13. The method according to any one of claims 1 to 12, wherein, C6-C8 aromatic hydrocarbons are separated from stream S6 by extractive distillation in at least one aromatic hydrocarbon extraction unit (AEU).

14. The method according to any one of claims 1 to 13, wherein, The stream S5 is converted into syngas in at least one gasifier and / or partial oxidation reaction unit and / or the stream S8 is further subjected to a cracking process selected from catalytic cracking, thermal cracking and steam cracking.

15. The method according to any one of claims 1 to 14, further comprising the following additional steps: - To obtain monomers, polymers or polymer products by means of C6-C8 aromatic hydrocarbons that are available or obtainable by any one of claims 1 to 14; and / or syngas that are available or obtainable by claim 14; and / or chemical materials that are available or obtainable by any one of claims 1 to 14, preferably by subjecting the stream S8 to the cracking process and converting it with chemical materials that are available or obtainable by claim 14.

16. The method according to claim 15, wherein, The monomer is a diol or polyol, preferably butanediol; an aldehyde, preferably formaldehyde; a diisocyanate or polyisocyanate, preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylene diisocyanate (HDI) or isophorone diisocyanate (IPDI); an amide, preferably caprolactam; Olefins, preferably styrene, ethylene and norbornene; alkynes; (di) esters, preferably methyl methacrylate; monoacids or diacids, preferably adipic acid or terephthalic acid; diamines, preferably hexamethylenediamine or nonanediamine; or sulfones, preferably 4,4'-dichlorodiphenyl sulfone.

17. The method according to claim 15 or 16, wherein, The polymer and / or the polymer product contains polyamide (PA), preferably PA 6 or PA 66; polyisocyanate addition polymers, preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), polyacrylonitrile butadiene styrene (ABS), polystyrene acrylonitrile (SAN), polyacrylate styrene acrylonitrile polyacrylate (ASA), polytetrafluoroethylene (PTFE), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis-1,4-isoprene), poly(trans-1,4-isoprene) Poly(pentadiene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate (PBAT), polyester (PES), polyethersulfone (PESU), polyhydroxyalkanoate (PHA), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyetheretherketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); or copolymers or mixtures thereof.

18. The method according to any one of claims 15 to 17, wherein, The polymer and / or the polymer product are then converted into the following or a portion thereof: - Automotive parts, preferably cylinder head covers, engine hoods, turbocharger housings, turbocharger baffles, intake pipes, intake manifolds, connectors, gears, fan wheels, coolant tanks, housings, heat exchanger housing parts, coolant coolers, turbocharger coolers, thermostats, water pumps, radiators, fasteners, battery system parts for electric vehicles, dashboards, steering column switches, seats, headrests, center consoles, transmission components, door modules, A, B, C, or D pillar covers, spoilers, door handles, exterior mirrors, windshield wipers, windshield wiper protection housings, decorative grilles, cover strips, roof rails, window frames, sunroof frames, antenna panels, headlights and taillights, engine hoods, cylinder head covers, intake manifolds, airbags, cushioning pads or coatings; - Fabrics, preferably shirts, trousers, sweaters, boots, shoes, shoe soles, bodysuits or jackets; - Electrical components, preferably electrical or electronic passive or active components, circuit boards, printed circuit boards, housing components, foil, wire, switches, plugs, sockets, distributors, relays, resistors, capacitors, inductors, spools, lamps, diodes, LEDs, transistors, connectors, voltage regulators, integrated circuits (ICs), processors, controllers, memory, sensors, microswitches, micro buttons, semiconductors, reflector housings for light-emitting diodes (LEDs), fasteners, gaskets, bolts, strips, slide-in guides, screws, nuts, membrane hinges, spring hooks (clamp-in) or spring tongues; - Consumer goods, agricultural products, or pharmaceutical products, preferably tennis strings, climbing ropes, bristles, brushes, artificial turf, 3D printed filaments, lawnmowers, zippers, hook and loop fasteners, paper machine fabrics, extrusion coatings, fishing lines, fishing nets, offshore lines and ropes, vials, syringes, ampoules, bottles, sliding elements, spindle nuts, chain conveyors, sliding bearings, rollers, wheels, gears, ring gears, screws and spring dampers, hoses, pipes, cable sheaths, sockets, switches, cable ties, fan wheels, carpets, cosmetic boxes or bottles, mattresses, cushioning pads, insulating materials, detergents, dishwasher detergent blocks or powders, shampoos, shower gels, bath gels, soaps, fertilizers, fungicides, or pest control agents; - For packaging in the food industry, single-layer or multi-layer blown film, cast film (single-layer or multi-layer), biaxial stretch film, or laminated film are preferred; or - Structural components, preferably rotor blades, insulating materials, frames, housings, walls, coatings, or partition walls.

19. The method according to any one of claims 15 to 18, wherein, The content of the liquid stream S1 in the monomer, polymer, or polymer product is 1 wt% or more, preferably 2 wt% or more, more preferably 5 wt% or more, more preferably 15 wt% or more, more preferably 30 wt% or more, more preferably 40 wt% or more, more preferably 60 wt% or more, more preferably 80 wt% or more, more preferably 90 wt% or more, more preferably 95 wt% or more; and / or wherein the content of the liquid stream S1 in the monomer, polymer, or polymer product is 100 wt% or less, preferably 95 wt% or less, more preferably 90 wt% or less, more preferably 50 wt% or less, more preferably 25 wt% or less, more preferably 10 wt% or less; and preferably wherein the content is determined based on a source retention and / or separation and / or quality balance and / or certificate declaration chain of custody model, preferably based on quality balance, preferably according to the International Sustainability and Carbon Certification (ISCC) standard.

20. A chemical apparatus for separating C6-C8 aromatic hydrocarbons from a liquid stream containing at least one type of plastic pyrolysis oil, the apparatus comprising... (i) at least one first hydrogenation processing unit HU1, the at least one first hydrogenation processing unit HU1 comprising at least one inlet and at least one outlet. (ii) Optionally, a recirculation unit is located downstream of and fluidly connected to the inlet and outlet of the first hydrogenation treatment unit HU1. (iii) A distillation unit DU, which is downstream of and fluidly connected to the outlet of the first hydrogenation treatment unit HU1, the at least one distillation unit having a bottom outlet BO and a top outlet HO. (iv) A second hydrogenation treatment unit HU2, which is downstream of and fluidly connected to the top outlet HO of the at least one distillation unit DU. (v) At least one aromatic hydrocarbon extraction unit AEU, which is downstream of and fluidly connected to the second hydrogenation treatment unit HU2.

21. Use of the chemical equipment according to claim 20 for the method according to any one of claims 1 to 19.

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