Process for separating a high boiling fraction from a plastic waste pyrolysis effluent

Abstract

The invention concerns a process and a plant for separating a high boiling fraction from a plastic waste pyrolysis effluent. The plastic waste pyrolysis effluent is brought into physical contact with a fraction of the condensed plastic waste pyrolysis effluent whereby the high boiling fraction is separated and can be used as a feedstock for further processes such as partial oxidation. Further fractions of the plastic waste pyrolysis effluent are then separated by condensation and are suited as feedstock for a steam cracking process in a steam cracking unit.

Description

Process for separating a high boiling fraction from a plastic waste pyrolysis effluentTechnical areaThe present invention relates to pyrolysis oils made by pyrolysis from plastic waste and their use for processes such as steam cracking.Background of the inventionFull range pyrolysis oils made by pyrolysis from plastic waste such as mixed plastic waste and / or end-of life tires are not applicable for conversion in a steam cracker because of their final boiling point FBP which is too high for said utilization. Such steam cracking processes require feedstocks having a final boiling point, depending on the specific layout of the process, of no more than 380 °C or less, such as 360 °C, 340 °C or even no more than about 200 °C. In contrast, full range pyrolysis oils have a final boiling point FBP of >>380 °C, for example above 500 °C.The high final boiling point is one of the crucial problems because the whole feedstock (e.g., the pyrolysis oil) must be evaporated in a steam stream before fed into the cracking section of a steam cracking process to avoid fouling and plugging. Due to the upper limit for the final boiling point FBP of such feedstocks for steam cracking processes discussed in the previous paragraph, said required evaporation of the feedstock cannot be archived with such full range pyrolysis oils as feedstock. Hence, some means of fractionation in front of the cracking section of steam cracking processes is required when using full range pyrolysis oils as feedstock for a steam cracking process to obtain a pyrolysis oil fraction having the desired final boiling point FBP.Such fractionation usually comprises one or more distillation and / or condensation process steps which are energy consuming, require expensive equipment and maintenance caused by fouling and / or plugging.CN 109456787 A relates to the field of waste tire processing, and to a device and a method for processing waste tires by thermal cracking. The device comprises an oil and gas quencher connected to the outlet of a Roots blower, which Roots blower is connected to the outlet of a pyrolysis reactor. The “hot oil” and the “cold cracking oil” are mixed in said oil and gas quencher for rapid cooling. The material enters after rapid cooling an “oil and gas condenser” for condensation, and the gaseous product obtained after condensation is non-condensable gas. No liquid fraction such as the high boiling fraction is separated therefrom in said oil and gas quencher. Accordingly, the whole range of liquid products from the pyrolysis, including the high boiling fraction, are condensed as a single fraction in the “oil and gas condenser”. Therefore, further energy-consuming separation steps are required to obtain from said condensed pyrolysis oil a liquid fraction which has a final boiling point suited for conversion in a (steam) cracking unit.WO 2023 / 200961 A1 describes systems and processes for converting waste plastics and other waste materials to useful end products. A pyrolysis oil fraction may be used as a quench medium, lowering the temperature of the pyrolysis reactor effluent and slowing or halting any post reactions (e.g., limit the production of light gases such as methane) that may otherwise occur during transport to the separation system. The high boiling fraction of saidpyrolysis reactor effluent is not separated therefrom in this part of the systems and processes described therein. Liquid fractions are only separated from the pyrolysis reactor effluent afterwards in a separation system which comprises energy consuming unit operations such as distillation. Accordingly, a feedstock suited for cracking processes such as steam cracking is only formed by energy consuming unit operations such as distillation.US 2022 / 186121 A1 relates to a process for preparation of a lubricant base stock from the thermal decomposition of plastic polymer. The process comprises a multistage condensation comprising a plurality of condensation stages which immediately follows a pyrolysis step. The first condensation stage is preferably a quench tower using a coolant liquid such as supercritical carbon dioxide, water or aqueous solutions and hydrocarbon-based coolants such as glycol and liquid propane. US 2022 / 186121 A1 further describes condensation of a tar and water together from pyrolysis products in a quench unit (Figure 2 in said document). Accordingly, a “coalescenser / separator (24)” is required to separate tar and water downstream of the quench unit. Water co-condensed with tar comprises a high portion of undesired components such polycyclic aromatics of which at least a portion remains dispersed in the waste water after separation of tar and water in said “coalescenser / separator (24)”.US 2018 / 187087 A1 relates to systems and methods for processing waste plastic in which a melt of plastic materials is subjected to a pyrolysis and the hydrocarbon gas stream obtained therefrom is condensed to a hydrocarbon-based product. At least a portion of the light fraction of said product may be used as a quench medium in said condensation in a quench unit. Thereby, the light fraction evaporates in the quench unit. The re-condensation of the light fraction after vaporization in the quench unit requires stronger cooling in comparison to a quench medium having a higher boiling point range such as a medium boiling fraction. Accordingly, more complex means for cooling are required and the energy consumption for re-condensation of the quench medium “light fraction” is high.US 2023 / 279298 A1 relates to separation systems and related methods for use in processing organic polymer feed materials such as plastics to form pyrolysis oil, comprising a novel condensation approach. Said condensation approach comprises a first condenser which may be a quench tower which uses (a portion of) the liquid separated in said first condenser as quench medium. Hence, at least a portion of the pyrolysis oil heavy fraction is utilized as quench medium. Such pyrolysis oil heavy fraction usually comprises a higher concentration of undesired components such as dienes and / or compounds comprising one or more heteroatom. Such undesired components accumulate during use of said heavy fraction as quench medium therein. Furthermore, such heavy fraction of pyrolysis oils may also comprise particles which cause abrasive damage in the spray nozzles of a quench unit. Such abrasive damage results in a pressure drop of the quench medium which then is not sufficiently sprayed into the desired space inside the quench unit and thereby quenching of the pyrolysis gas is incomplete.It is an objective to provide a process for converting a full range pyrolysis oil made by pyrolysis from plastic waste into a stream suited for feeding into the cracking section of a steam cracking process.It is a further objective to provide a process for adjusting the final boiling point FBP of a full range pyrolysis oil made by pyrolysis from plastic waste whereby fouling and / or plugging are avoided.It is a further objective of the present invention to provide an efficient and economic process for separating the high boiling fraction from the medium- and low boiling fractions of a pyrolysis oil made by pyrolysis from plastic waste.It is a further objective of the present invention to provide a feed stream suited for synthesis gas production by partial oxidation from an unrefined full range pyrolysis oil made by pyrolysis from plastic waste.It is a further objective of the present invention to reduce the fraction of unrefined full range pyrolysis oil which requires a further refining (e.g., removal of heteroatoms) for utilization in a steam cracking process while utilizing the remaining fraction of said unrefined full range pyrolysis oil for synthesis gas production by partial oxidation.Summary of the inventionThese objectives are solved by a process for separating a high boiling fraction from a plastic waste pyrolysis effluent, said process comprising the steps(i) providing a feed stream S1 , wherein said feed stream S1 comprises or preferably consists of plastic waste,(ii) converting said feed stream S1 by pyrolysis in at least one pyrolysis unit PU into a solid residue S3 and a gaseous pyrolysis effluent S2, wherein said gaseous pyrolysis effluent S2 comprises a high boiling fraction S5, a medium boiling fraction S6, a low boiling fraction S8, a non-condensable stream S7 and optionally water,(iii) quenching said gaseous pyrolysis effluent S2 in at least one quench unit QU with a quench medium QM and thereby forming a first intermediate stream S4, wherein said gaseous pyrolysis effluent S2 and said quench medium QM are physically contacted in the at least one quench unit QU, and wherein said first intermediate stream S4 comprises a liquid and a gaseous phase, wherein said quench medium QM is selected from the group consisting of second medium boiling fraction S6b optionally separated in step (vii), medium boiling fraction S6 condensed and separated in step (v), mixtures thereof, and mixtures thereof further comprising at least one further oil FO, wherein said first intermediate stream S4 has a temperature of 180 to 350 °C when leaving the at least one quench unit QU,(iv) separating said liquid and a gaseous phase comprised in said first intermediate stream S4, wherein said liquid phase comprises or consists of said high boiling fraction S5, and wherein said gaseous phase comprises or consists of a second gaseous intermediate stream S4',(v) condensing and separating a fraction of said second gaseous intermediate stream S4' in a first condensation unit CU1 , wherein said condensed and separated fraction comprises or consists of said medium boiling fraction S6, and wherein the remaining gaseous fraction of said second gaseous intermediate stream S4' comprises or consists of a third gaseous intermediate stream S4",(vi) condensing and separating a fraction of said third intermediate stream S4" in a second condensation unit CU2, wherein said condensed and separated fraction comprises or consists of said low boiling fraction S8 and optionally water, and wherein and the remaining gaseous fraction of said third gaseous intermediate stream S4" comprises or consists of said non-condensable stream S7,(vii) optionally separating said medium boiling fraction S6 in a splitting unit SPU into at least two portions, wherein the first portion is a first medium boiling fraction S6a, wherein the second portion is a second medium boiling fraction S6b, and wherein said second medium boiling fraction S6b is physically contacted in step (iii) as quench medium QM with the gaseous pyrolysis effluent S2 in the at least one quench unit QU, and(viii) optionally combining the first medium boiling fraction S6a and the low boiling fraction S8 in a mixing unit MU to obtain a stream S9.These objectives are further solved by a pyrolysis plant for separating a high boiling fraction from a plastic waste pyrolysis effluent, the plant comprising a) at least one pyrolysis unit PU, b) at least one quench unit QU, wherein said at least one quench unit QU is downstream of and fluidically connected to said at least one pyrolysis unit PU, c) at least one separation unit SU, wherein said at least one separation unit SU is downstream of and fluidically connected to said at least one quench unit QU, d) at least one first condensation unit CU1 , wherein said at least one first condensation unit CU1 is downstream of and fluidically connected to said at least one separation unit SU, e) at least one second condensation unit CU2, wherein said at least one second condensation unit CU2 is downstream of and fluidically connected to said at least one first condensation unit CU1 , f) at least one splitting unit SPU, wherein said at least one splitting unit SPU is downstream of and fluidically connected to said at least one first condensation unit CU1, and g) optionally at least one mixing unit MU, wherein said at least one mixing unit is downstream of and fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2.The high boiling fraction of the pyrolysis oil PO can be separated therefrom by an energy efficient method using the at least one quench unit QU and the medium boiling fraction S6b or the medium boiling fraction S6 as quench medium QM which quench medium QM is directly contacted with the gaseous pyrolysis effluent S2 in the at least one quench unit QU. Thereby, the high boiling fraction S5 is separated from the gaseous pyrolysis effluent S2.The disadvantages of known processes discussed above can be avoided by at least one quench unit located in between the pyrolysis unit and the further condensation units in which at least one quench unit the high boiling components of the full range pyrolysis oil are removed to reach the final boiling point required for application in a steam cracking process.Furthermore, solid particles passed though the pyrolysis unit and, hence, comprised in the gaseous pyrolysis effluent S2 are also separated therefrom in the at least one quench unit. Such undesired solid particles comprise solid residue S3 and / or solid particles such as catalysts added to the pyrolysis process in the pyrolysis unit PU.To recover and use the energy from cooling down and condensation of the gaseous pyrolysis effluent S2 in a heat recovery section is very problematic caused by the high dienic and olefinic components concentration and so fouling and plugging problems. Such conventional heat recovery sections rely on heat exchangers which comprise heattransfer surfaces prone to fouling and plugging due to dienes and other polymerizable components comprised in pyrolysis oils made by pyrolysis from plastic waste.A separation of the high boiling fraction and adjustment of the final boiling point of the pyrolysis oil without additional heat demand and heat-transfer surfaces is feasible by the process according to the present invention. Thereby, undesired fouling and plugging caused by dienes and other polymerizable components comprised in pyrolysis oils made by pyrolysis from plastic waste is reduced or even omitted.The invention omits problems caused when using the light fraction or the heavy fraction of plastic waste pyrolysis oil. Instead, the utilization of the medium boiling fraction S6(b), optionally mixed with at least one further oil FO, enables a rather simple set up of units, results in a waste water stream S10 comprising less contaminants and avoids accumulation of undesired components such as dienes and compounds comprising one or more heteroatom. Furthermore, water is not co-condensed with heavy fraction S5, whereby no additional unit is required for separating (waste) water from stream S5. Rather, stream S5 is directly suited as a feedstock for partial oxidation whereby valuable synthesis gas comprising CO and H2is produced.Co-condensation of water with stream S5 in the at least one quench unit QU is omitted by setting the flow rate of quench medium QM. Said flow rate is adapted to the flow rate and compositional characteristics of pyrolysis gas fed into the at least one quench unit QM. Said quench medium QM flow rate is unambiguously adjusted by the skilled person until the first intermediate stream S4 has the desired temperature of 180 to 350 °C, preferably 200 to 280 °C and more preferably 230 to 270 °C when leaving the at least one quench unit QU. When matching said temperature of S4, the required flow rate of the quench medium QM is set and the process delivers the desired results among those, water is not condensed together with stream S5 in the one or more quench unit QU and is only condensed in the second condensation unit CU2.A feed stream suited for synthesis gas production by partial oxidation (stream S5) from an unrefined full range pyrolysis oil made by pyrolysis from plastic waste is provided by the process according to the present invention. This fraction of the pyrolysis oil may require no further, energy intensive upgrading process steps such as removal of heteroatoms. At the same time, a lower fraction of the full range pyrolysis oil requires to be condensed in condensation units. Thereby further energy can be saved.FiguresFigure 1 shows the process for separating a high boiling fraction from a plastic waste pyrolysis effluent and the pyrolysis plant according to the present invention with quench medium QM = stream S6b.Figure 2 shows the process for separating liquid fractions from a plastic waste pyrolysis effluent according to prior art which also represents the process flow scheme used for comparative example 1.Figure 3 shows the process for separating liquid fractions from a plastic waste pyrolysis effluent according to prior art which also represents the process flow scheme used for comparative example 2.Detailed description of the inventionThe present invention is further described below with reference to the embodiments, but the present invention is not limited to these embodiments, and any modifications of these embodiments, combinations of these embodiments or substitutions within the basic spirit of the present invention are still within the scope of the present invention as claimed.Definitions:In the context of the present description and the accompanying claims, the term “about” preferably means a deviation of the thus described value of ±10 %. In the context of the present invention, the term “combinations thereof” is inclusive of one or more of the recited elements. In the context of the present invention, the term “mixture thereof” is inclusive of one or more of the recited elements.“ppmw” is defined herein as a parts-per-million notation referring to a mass fraction.“Final boiling points” (FBP) are determined according to ASTM D86-23.“Unrefined pyrolysis oil” are defined herein as pyrolysis oils made by pyrolysis from plastic waste which comprise all condensable reaction products from said pyrolysis.“Full range pyrolysis oil” are defined herein as pyrolysis oils made by pyrolysis from plastic waste which comprise the full range of condensable compounds, also high boiling compounds, formed during the pyrolysis process. The high final boiling point FBP (determined according to ASTM D-86-23) is a result of such high boiling components present in such “full range pyrolysis oils”.The term “downstream of” is defined herein in respect to a succession of unit operations as located next to each other and on the side which is in the flow direction of fluids passing said succession of unit operations.The term “fluidically connected to” in respect to two or more units is defined herein that a fluid such as a particulate solid, liquids, gases, and mixtures thereof can flow from one of such unit to the other such unit and flow throughand / or along such an analytical unit. Two units “fluidically connected to” each other are for example connected by one or more pipes which each other or by screw conveyors or by extruders or by solids pumps.“Directly” in respect to “fluidically connected” is defined herein as fluidically connected by a suitable means such as a pipe. Accordingly, the respective outlet of a first unit is fluidically connected by a suitable means such as a pipe with the respective inlet of a second unit wherein said second unit is downstream of said first unit.“Indirectly” in respect to “fluidically connected” is defined herein as interrupted by e.g., an additional unit, storage tank(s), transportation of a stream by for example truck or train or in a pipeline.“Condensing” is defined herein as follows: a liquid stream is separated from a gaseous stream by reducing the temperature of said gaseous stream. Boiling points of fractions comprised in the gaseous pyrolysis effluent S2 are determined by ASTM-D86-23. “D86-0 %” represents the initial boiling point IBP of the respective fraction (“0 Vol.-% FBP”), “D86-50 %” the determined boiling point when 50 Vol.-% of the respective fraction are vaporized and “D86- 100” the final boiling point FBP of the respective fraction (“100 Vol.-% FBP”).A first aspect of the process and the plant according to the present invention are shown in Figure 1 . The labeling in Figure 1 is also used in the following description.In step (i) of the process according to the present invention, a feed stream S1 is provided. Said first feed stream S1 comprises or preferably consists of plastic waste. In the context of the present invention, the term “plastic waste” preferably refers to any plastic material discarded after use, i.e., the plastic material has reached the end of its useful life and is considered post-consumer waste. The plastic waste can be pure polymeric plastic waste, mixed plastic waste or film waste, including soiling, adhesive materials, fillers, residues etc. The plastic waste may have an oxygen content, a nitrogen content, sulfur content, halogen content and optionally also a heavy metal content. The plastic waste can originate from any plastic material containing source. The term “plastic waste” also includes industrial and domestic plastic waste and further including used tires (“end-of-life tires”) and agricultural and horticultural plastic material.Typically, plastic waste is a mixture of different plastic materials, including hydrocarbon plastics, e.g., polyolefins such as polyethylene (HDPE, LDPE) and polypropylene, polystyrene, copolymers comprising styrene units, etc. Plastic waste may further comprise polymers composed of carbon, hydrogen, and other elements such as chlorine, fluorine, oxygen, nitrogen, sulfur, silicone, etc., for example chlorinated plastics, such as polyvinylchloride (PVC), polyvinylidene chloride (PVDC), etc., nitrogen-containing plastics, such as polyamides (PA) (e.g., poly-(azepan-2- one) (PA6), poly[imino(1,6-dioxohexamethylene) iminohexamethylene) (PA66)), polyurethanes (PU), acrylonitrile- butadiene-styrene (ABS), etc., oxygen-containing plastics such as polyesters, e.g., polyethylene terephthalate) (PET), poly(oxy-1 ,4-butanediyloxycarbonyl-1,4-phenylenecarbonyl) (PBT), polycarbonate (PC), polyoxymethylene (POM), silicones and / or sulfur bridges crosslinked rubbers.Accordingly, the feed stream S1 comprises at least one polymer selected from the group comprising or preferably consisting of polyolefins, polystyrene, copolymers comprising styrene units, polyvinylchloride, polyvinylidene chloride, polyamides, polyurethanes, polyesters, polycarbonate, polyesters, rubbers, and mixtures thereof.Typically, the plastic material(s) comprises additives, such as processing aids, plasticizers, flame retardants, pigments, light stabilizers, lubricants, impact modifiers, antistatic agents, antioxidants, etc. These additives may comprise elements other than carbon and hydrogen. For example, bromine is mainly found in connection to flame retardants. Heavy metal compounds may be used as lightfast pigments and / or stabilizers in plastics. Cadmium, zinc, and lead may be present in heat stabilizers and slip agents used in plastics manufacturing. The plastic waste can also contain residues. Residues in the sense of the invention are contaminants adhering to the plastic waste. One example of “residues” is bio waste. The additives and residues are usually present in an amount of less than 50 wt.- %, preferably less than 30 wt.-%, more preferably less than 20 wt.-%, even more preferably less than 10 wt.-%, based on the total weight of the dry weight plastic.Examples of rubber waste (which is also considered “plastic waste” in the sense of the present invention) include end-of-life tires, rubber waste produced during manufacturing processes and discarded rubber containing products such as latex examining gloves and gaskets. End-of-life tires comprise further ingredients such as textiles and organic and inorganic additives which may be separated from the rubber portion of end-of-life tires prior to pyrolysis.Examples of bio waste which can be comprised in “plastic waste” as residue include green waste, food waste, human waste, manure, sewage, sewage sludge and slaughterhouse waste.In step (ii) of the process according to the present invention, said feed stream S1 is converted by a pyrolysis in at least one pyrolysis unit PU into a solid residue S3 and a gaseous pyrolysis effluent S2. Said gaseous pyrolysis effluent S2 comprises a high boiling fraction S5, a medium boiling fraction S6, a low boiling fraction S8, a noncondensable stream S7 and water.The term “pyrolysis” includes slow pyrolysis, fast pyrolysis, flash catalysis and catalytic pyrolysis. These pyrolysis types differ regarding process temperature, heating rate, residence time, feed particle size, etc. resulting in different product quality. The pyrolysis unit may be operated adiabatically, isothermally, nonadiabatically, non-isothermally, or combinations thereof. The pyrolysis reactions of this disclosure may be carried out in a single stage or in multiple stages. For example, the pyrolysis unit can comprise two reactor vessels fluidically connected in series.To obtain the gaseous pyrolysis effluent S2 in step (ii), the feed stream S1 is inserted into at least one pyrolysis unit PU using a dosing unit such as a screw or an extruder or a rotary valve or a pneumatic conveyor or a liquid injector. The feed stream S1 is optionally pre-heated in e.g., a heat exchanger prior to insertion into the at least one pyrolysis unit PU and / or subjected to a pre-pyrolysis (“pre-heating”) at a temperature in the range of, for example, from about200 to about 400 °C. Next, the feed stream S1 is heated in the at least one pyrolysis unit PU to a temperature in the range of from about 250 to about 900 °C, more preferably 300 to 700 °C and most preferably 350 to 550 °C, and a pressure in the range of from about 0.5 to about 2 bar(abs), more preferably in the range of from 0.9 to about 1 .5 bar(abs). Preferably, the pyrolysis is performed in the pyrolysis unit PU under an inert atmosphere exempt of oxygen or air. Accordingly, said pyrolysis is not related to hydrolysis and other solvolysis processes used for depolymerization of polymers. Such processes require different process conditions, i.e., a pressure far above 2 bar(abs.) and or the presence of purposely added water and / or oxygen which result in an atmosphere which is not to be considered “inert”. Pyrolysis processes as such are known. They are described, e.g., in EP 0713906 A1, WO 95 / 03375 A1 and Jorg Woidasky, Ullmanns Encyclopedia of Industrial Chemistry, chapter 5.2.1 “Pyrolysis”, pages 15-17, 2020 Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim (DOI: 10.1002 / 14356007.a21 _057.pub2).The at least one pyrolysis unit PU is preferably selected from the group comprising or more preferably consisting of fluidized bed reactors, moving bed reactors, entrained flow reactors, screw reactors, extruders, stirred tank reactors and rotary kiln reactor. Most preferably, the at least one pyrolysis unit PU comprises a reactor chamber which has preferably a cylindrical shape (e.g., a tube), and a rotation mechanism inside said reactor chamber. Said rotation mechanism is preferably selected from the group comprising or more preferably consisting of conveyor screws, double conveyor screws, fluidization units and combinations thereof. Said pyrolysis unit PU is particularly suited to convert said feed stream S1 into a solid residue S3 and a gaseous pyrolysis effluent S2 in step (ii).A first particularly preferred example of said preferred pyrolysis unit PU is described in the following ("PUT'): The feed stream S1 is preferably converted into a solid residue S3 and a gaseous pyrolysis effluent S2 in step (ii) in a pyrolysis unit PU1 , said pyrolysis unit PU1 comprises a reactor chamber, preferably a cylindrical reactor chamber, further comprising a rotation mechanism inside said reactor chamber which ensures an intensive whirling motion inside said reactor chamber. Furthermore, (solid) particles P are preferably added to said pyrolysis unit PU1 together with or separate of the feed stream S1. Said particles P form a moving bed inside the reactor chamber set into a whirling motion by intensive stirring during operation of said reactor. Thereby, enough thermal energy is provided for the pyrolysis reaction. The pyrolysis unit PU1 enables an efficient separation of inorganic from organic components comprised in the feed stream S1 . Furthermore, the pyrolysis unit PU1 allows stable pyrolysis reaction conditions also for a feed stream S1 having an inhomogeneous composition. Furthermore, no external heating of a pyrolysis unit PU1 is required during step (iii). Such particularly preferred pyrolysis units PU1 are for example disclosed in WO 98 / 39368 A1, WO 9809997 A1, WO 2023 / 214881 A1 , WO 2014 / 51514 A1 and DE 102012022710 B4. Said particularly preferred type of pyrolysis unit, pyrolysis unit PU1, is described in more detail below:The pyrolysis unit PU1 preferably comprises a feeding system which can be any type of equipment suited to feed the feed stream S1 into the reactor chamber of said pyrolysis unit PU1. Suitable feeding systems are for example one or more pumps, screws, extruders, locks, and combinations thereof. Such feeding systems are well known in the art and can be adapted to a given reaction chamber by a skilled person. The feed stream S1 and / or the particles P inserted into the reactor chamber are optionally preheated, preferably to a temperature in the range 100 to 450 °C,more preferably 150 to 350 °C. Particles P are for example selected from inert particles such as sand, catalysts such as zeolites, adsorbents, and mixtures thereof. The diameter of particles P preferably ranges from 3x104to 3x102m. The amount of particles P may be up to 50 wt.-% or higher, preferably up to 30 wt.-% and more preferably up to 15 wt.-% based on the weight of the mixture of feed stream S1 , particles P and other substances inside the reactor chamber.The reactor chamber (also referred to as “stator”) is preferably cylindrical and comprises at least one inlet for feeding the feed stream S1 and particles, either to the same or separate inlets. Said at least one inlet is upstream of and fluidically connected to the feeding system. The reactor chamber further comprises at least one outlet to purge the reaction products. Preferably, the reactor chamber comprises separate outlets for purging the gaseous pyrolysis effluent S2 and solid residue S3 and / or particles P. Said at least one outlet or at least two outlets are fluidically connected to a condensation system for the pyrolysis gas and / or a solids separation system which is / are downstream of the reactor chamber. The reactor chamber can be double-walled and comprise a heat-transfer system.Pyrolysis unit PU1 further comprises a rotation mechanism (“rotor”) which is connected to the reactor chamber (“stator”). Such pyrolysis unit PU1 are also known as “rotor-stator reactors”. Said rotation mechanism is preferably located rotably in the faces of the reactor chamber. Said rotation mechanism comprises a shaft, said shaft being connected to a drive for rotating said shaft. Said rotation mechanism is oriented coaxially with the axis of the (cylindrical) reactor chamber. Said rotation mechanism comprises fluidization units, preferably radially extending fluidization units. Said fluidization units are preferably selected from the group comprising or preferably consisting of hammers, knives, blades, wings, discs, and combinations thereof. Optionally, vanes are symmetrically attached by means of discs to the shaft of the discs. The fluidization units may be of equal length, or optionally of alternating lengths. The pyrolysis unit PU1 may be part of a hammer mill and, preferably, step (ii) of the process according to the present invention is carried out in a hammer mill. The peripheral speed of the extending fluidization units during operation of the pyrolysis unit PU1 preferably ranges from 15 to 135 m / s, more preferably from 35 to 85 m / s. The rotating speed of the shaft is preferably at least 350 rpm, more preferably at least 400 rpm. The shaft rotating speed preferably is up to 900 rpm, more preferably up to 700 rpm. Optionally, one or more of water, steam, hydrogen, and ammonia are co-fed into the reaction chamber of the pyrolysis unit PU1 .A second particularly preferred example of said preferred pyrolysis unit PU is described in the following (“PU2”): The feed stream S1 is preferably converted into a solid residue S3 and a gaseous pyrolysis effluent S2 in step (ii) in a pyrolysis unit PU2 which comprises a reactor chamber and a rotating mechanism wherein said rotating mechanism comprises one or more conveyor screw(s), more preferably, said rotating mechanism comprises a conveyor double screw. Optionally, at least one chain is disposed on the conveyor screw or conveyor double screw and / or the conveyor screw or conveyor double screw comprises at least one screw flight. Pyrolysis units PU2 are for example described in detail in WO 2021 / 254550 A1, WO 2024 / 068818 A1, and WO 2024 / 068820 A1 .Furthermore, (solid) particles P are preferably added to said pyrolysis unit PU2 together with or separate of the feed stream S1. Said particles P can be for example sand, silicon carbide, calcium oxide, calcium hydroxide and combinations thereof. Such added particles P can transfer heat to the feed stream S1 and / or capture halogens which may be set free from the feed stream S1 during pyrolysis. Preferably, said pyrolysis unit PU2 is electrically heated, more preferably with electricity from renewable sources. The residence time for the feed stream S1 inside the pyrolysis unit PU2 preferably range from 2.5 to 40 min. The residence time inside the pyrolysis unit PU2 for the gaseous pyrolysis effluent S2 formed by the pyrolysis reaction from feed stream S1 preferably ranges from 5 to 40 s. More preferably said gaseous pyrolysis effluent S2 formed by the pyrolysis reaction from feed stream S1 is sequentially separated from said pyrolysis unit PU2, most preferably through bult-in filter elements.Next, in step (iii) said gaseous pyrolysis effluent S2 is cooled in at least one quench unit QU wherein the liquid second medium boiling fraction S6b or the liquid medium boiling fraction S6 (denoted “quench medium QM” and described in detail further below) is physically contacted with said gaseous pyrolysis effluent S2 in said at least one quench unit QU as quench medium QM. Thereby, a high boiling fraction S5 is condensed from said gaseous pyrolysis effluent S2 said in said at least one quench unit QU. Thereby, also a first intermediate stream S4 is formed which is not condensed in said at least one quench unit QU and comprises the second medium boiling fraction S6b and those portions of the gaseous pyrolysis effluent S2 which are not condensed in said at least one quench unit QU. The gaseous pyrolysis effluent S2 is cooled by direct heat exchange in the at least one quench unit QU by physically contacting said gaseous pyrolysis effluent S2 inside said at least one quench unit QU with the quench medium QM which is a liquid when entering said at least one quench unit QU. Accordingly, said gaseous pyrolysis effluent S2 and said quench medium QM are in physical contact with each other inside the at least one quench unit QU. Said high boiling fraction S5 and said first intermediate stream S4 form a liquid / gas mixture directly in said at least one quench unit QU.The quench medium QM is selected from the group comprising or preferably consisting of liquid second medium boiling fraction S6b, the liquid medium boiling fraction S6, at least one further oil FO, and mixtures thereof.The process utilizing the liquid second medium boiling fraction S6b as quench medium QM is shown in Figure 1.The quench medium QM comprises liquid second medium boiling fraction S6b and / or the liquid medium boiling fraction S6. Preferably, the quench medium QM consists of one member selected from the group consisting of liquid second medium boiling fraction S6b, the liquid medium boiling fraction S6, mixtures thereof, and mixtures thereof further comprising at least one further oil FO.Further oils FO are selected from the group comprising or preferably consisting of pyrolysis oils not formed by the process according to the present invention, the pyrolysis fuel oil fraction formed by steam cracking of hydrocarbons, fresh mineral lubricating oils, used mineral lubricating oils, bio-oils, oils formed by fluid catalytic cracking, oils formed by hydrocracking and combinations thereof.After the evaporation-condensation-equilibrium is reached, the liquid high boiling fraction S5 and the first intermediate stream S4 are separated in a separating unit SU. Said separation unit SU can be a stand-alone unit or included in the at least one quench unit QU. The separation process and suitable separation units will be described further below.The temperature of the first intermediate stream S4 when leaving said at least one quench unit QU determines the final boiling point of streams S6, S8 and S9. Said temperature of the first intermediate stream S4 is controlled by the amount and temperature of the quench medium QM. Accordingly, the following amounts of QM (given in wt.-% of gaseous pyrolysis effluent S2 which must be separated and used as quench medium QM (which amount is reduced in case a portion of the quench medium QM comprises at least one further pyrolysis oil FPO)) and the respective temperature ranges for streams S2, S4 and QM (S6 or S6b):Preferably, 20 to 70 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom. More preferably, 20 to 40 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom. A stream S9 having a final boiling point FBP in the range of about 180 to about 380 °C can be obtained in case 20 to 70 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom. A stream S9 having a final boiling point FBP in the range of about 340 to about 380 °C can be obtained in case 20 to 40 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom.The following temperature ranges for streams S2, S4 and QM (S6b or S6, optionally at least one further pyrolysis oil FPO added to S6b or S6) are preferably used to separate 20 to 70 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom to obtain a stream S9, wherein said stream S9 has a final boiling point FBP in the range of from 180 to 380 °C (determined according to ASTM D86-23):Said gaseous pyrolysis effluent S2 has a temperature of preferably 250 to 900 °C, more preferably 300 to 700 °C and most preferably 350 to 550 °C when entering the quench unit QU.The temperature of said quench medium QM (S6b or S6, optionally at least one further pyrolysis oil FPO added to S6b or S6) when physically contacted with said gaseous pyrolysis effluent S2 in said quench unit QU preferably ranges from 10 to 200 °C, more preferably 50 to 150 °C and most preferably 80 to 120 °C.Said first intermediate stream S4 has a temperature of preferably 180 to 350 °C, more preferably 200 to 280 °C and most preferably 230 to 270 °C when leaving the at least one quench unit QU.The following temperature ranges for streams S2, S4 and QM (S6b or S6, optionally at least one further pyrolysis oil FPO added to S6b or S6) are preferably used to separate 20 to 40 wt.-% of stream S2 are separated in step (iv) ashigh boiling fraction S5 therefrom to obtain a stream S9, wherein said stream S9 has a final boiling point FBP in the range of from 340 to 380 °C (determined according to ASTM D86-23):Said gaseous pyrolysis effluent S2 has a temperature of preferably 250 to 900 °C, more preferably 300 to 700 °C and most preferably 350 to 550 °C when entering the quench unit QU.The temperature of QM (S6b or S6, optionally at least one further pyrolysis oil FPO added to S6b or S6) when physically contacted with said gaseous pyrolysis effluent S2 in said quench unit QU preferably ranges from 10 to 200 °C, more preferably 50 to 150 °C and most preferably 80 to 120 °C.Said first intermediate stream S4 has a temperature of preferably 180 to 350 °C, more preferably 200 to 280 °C and most preferably 230 to 270 °C when leaving the at least one quench unit QU.The least one quench unit QU is fluidically connected to the outlet of the at least one pyrolysis unit PU through which the gaseous pyrolysis effluent S2 is purged. In case two sequentially arranged pyrolysis units PU1 and PU2, wherein PU2 is downstream of PU1, the at least one quench unit QU is fluidically connected to the outlet through which the gaseous pyrolysis effluent S2 is purged from PU2.Said at least one quench unit QU is selected from the group comprising or preferably consisting of tangential- injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of said quench medium QM, and counter-flow washers.Said quench unit QU preferably has at least a first inlet 11 and a second inlet I2, and at least a first outlet 01, wherein said gaseous pyrolysis effluent S2 enters said quench unit QU through said first inlet 11 , said quench medium QM enters said quench unit QU through said second inlet I2 and wherein said first intermediate stream S4 (mixed with said condensed stream S5) leaves said quench unit QU through said first outlet 01 .In step (iv) of the method according to the present invention, said condensed high boiling fraction S5 is separated as a liquid from said first intermediate stream S4 in a separation unit SU and thereby said first intermediate stream S4 is converted into a second gaseous intermediate stream S4'. Said second gaseous intermediate stream S4' comprises those fractions of the gaseous pyrolysis effluent S2 and the quench medium QM which are not condensed in the at least one quench unit QU, i.e., are kept in the gas phase.The high boiling fraction S5 comprises C11-C21 + hydrocarbons. The high boiling fraction S5 has an initial boiling point IBP (determined according to ASTM D86-23) of more than 170 °C, preferably of more than 180 °C and more preferably of more than 190 °C. The high boiling fraction S5 has a D86-50 % value (determined according to ASTM D86-23) of more than 330 °C, preferably of more than 350 °C and more preferably of more than 360 °C.Said second intermediate stream S4' is depleted in C11 -C21+ hydrocarbons compared to said first intermediate stream S4.The second gaseous intermediate stream S4' and the liquid high boiling fraction S5 may be separated from said first intermediate stream S4 by various methods known in the art which can be selected by the skilled person accordingly. Suitable methods for separation in step (iv) comprise gravity settling, centrifugal separation, inertial impaction and combinations thereof.The separation unit SU is selected from the group comprising or preferably consisting of gravity separators, centrifugal separators, filter vane separators, liquid / gas coalescers, and combinations thereof.Optionally, the at least one quench unit QU and said separation unit SU are combined in a quench and separation unit QSU.The liquid high boiling fraction S5 is suited as a feedstock or co-feedstock for a process selected from the group comprising or preferably consisting of partial oxidation, fluid catalytic cracking, hydrocracking, coking, visbreaking and other refining processes. The liquid high boiling fraction S5 can be blended with other feedstocks suited for said processes such as fossil and / or non-fossil feedstocks.Preferably, the liquid high boiling fraction S5 is used as a feedstock or co-feedstock for a partial oxidation process in at least one gasifier. The principal reaction product form such partial oxidation is synthesis gas (comprising CO and H2) which is an important feedstock for the chemical industry. Such partial oxidation reactions are known in the art and are for example disclosed in WO 2022 / 200532 A1 . The skilled person can select suitable reactors and reaction conditions to convert the liquid high boiling fraction S5 into synthesis gas by a partial oxidation process in at least one gasifier.Fluid catalytic cracking (FCC) is a process widely used in the petroleum refining industry to convert heavy hydrocarbon molecules comprised for example in pyrolysis oils made by pyrolysis from plastic waste, preferably the high boiling fraction of such pyrolysis oils, into lighter and more valuable products. In FCC, a catalyst is used to break down larger hydrocarbon molecules into smaller ones. The catalyst is usually a fine powder consisting of a zeolite compound, which is known for its cracking activity. The process takes place in a fluidized bed reactor, where the catalyst is suspended in a stream of oil vapor. This feedstock is mixed with hot catalyst in the reactor, and the mixture undergoes cracking at high temperatures (around 500 to 550 °C) and low pressures. Products of FCC comprise lighter hydrocarbons, such as gasoline, light olefins, and light cycle oil.Hydrocracking is a refining process used in the petroleum industry to convert heavy hydrocarbon feedstocks such as pyrolysis oils made by pyrolysis from plastic waste, preferably the high boiling fraction of such pyrolysis oils, into lighter, more valuable products. It is a combination of catalytic cracking and hydrogenation. The feedstock is mixedwith hydrogen gas and passed over a catalyst under high temperature and pressure. The catalyst used in hydrocracking is typically a combination of metal sulfides, such as molybdenum or tungsten, supported on an alumina or silica-alumina base.Coking is a thermal cracking process used in the petroleum refining industry to convert heavy residual oils such as pyrolysis oils made by pyrolysis from plastic waste, preferably the high boiling fraction of such pyrolysis oils, into lighter, more valuable products. It involves the application of heat to the feedstock in the absence of oxygen, which causes the breakdown of complex hydrocarbon molecules. Coking processes include delayed coking and fluid coking.Visbreaking is a process used in the petroleum industry to reduce the viscosity of oil such as pyrolysis oils made by pyrolysis from plastic waste. This process involves heating the oil to a high temperature, typically between 400 and 500 °C, for a specified amount of time. The high temperature breaks down long hydrocarbon chains in the oil, reducing its viscosity and making it easier to transport through pipelines. The visbreaking process can be done in a variety of equipment, including furnaces, heaters, and reactors. The process can also be done in combination with other refining processes, such as coking and hydrotreating.Other refining processes comprise isomerization processes, reforming processes, fractionation processes and the like.Suitable co-feedstocks for the liquid high boiling fraction S5 in a partial oxidation process are selected from the group comprising or preferably consisting of biomass, refuse-derived fuel (RDF), pyrolysis oils made from plastic waste, pyrolysis oils made from end of life tires, pyrolysis oils made from biomass, heating oils, vacuum residues, preferably vacuum distillation residues, crude oil residues, heavy crude oils, extra heavy crude oils, tar sand bitumen, visbreaker bottom residues, deasphalter bottom residues, C5 asphalthene fraction, high viscous residues, fuel oils, pyrolysis gasolines, waste oils, waste water, used oils, municipal solid waste (MSW), automotive shredder residue (ASR), coal, natural gas, industrial waste streams from other chemical processes than production of polymer dispersions, CO2 and mixtures thereof.In step (v) of the process according to the present invention, a fraction of said second gaseous intermediate stream S4' is condensed in a first condensation unit CU1 and thereby the medium boiling fraction S6 is separated as a liquid therefrom and the remaining gaseous part of said second gaseous intermediate stream S4' leaves said first condensation unit CU1 as third gaseous intermediate stream S4". The first condensation unit CU1 is downstream of and fluidically connected to the at least one separation unit SU.Said first condensation unit CU1 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense and combinations thereof.Said medium boiling fraction S6 comprises C6-C20 hydrocarbons. Said medium boiling fraction S6 has a final boiling point FBP (determined according to ASTM D86-23) of lesson more than 380 °C.In step (vi) of the process according to the present invention, said third intermediate stream S4" separated in step (v) from the second gaseous intermediate stream S4' is condensed in a second condensation unit CU2 and thereby a low boiling fraction S8 is separated as a liquid and said non-condensable stream S7 as a gas therefrom.Said second condensation unit CU2 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense and combinations thereof.Said low boiling fraction S8 comprises C6-C10 hydrocarbons. Said low boiling fraction S8 has a final boiling point FBP (determined according to ASTM D86-23) of preferably less than 230 °C, more preferably less than 230 °C and most preferably 210 °C.A water stream S10 is optionally also separated from the third intermediate stream S4" in the second condensation unit CU2.Said non-condensable stream S7 comprises C1 -C5 hydrocarbons, typical composition ranges are given below. The values for the individual components may be combined in any combination and preferably result in 100 wt.-% or less of the overall composition of stream S7 (because other and / or further components such as CO2 and / or H2S can be present in stream S7). The stream S7 preferably comprises methane in a concentration of 0.2 to 35 wt.-%, more preferably 0.4 to 30 wt.-% and most preferably 0.8 to 25 wt.-%. The stream S7 preferably comprises ethane and ethene (combined) in a concentration of 0.4 to 20 wt.-%, more preferably 0.8 to 15 wt.-% and most preferably 1.5 to 10 wt.-%. The stream S7 preferably comprises propane and propene (combined) in a concentration of 0.3 to 20 wt.- %, more preferably 0.5 to 18 wt.-% and most preferably 1 to 15 wt.-%. The stream S7 preferably comprises butanes, butenes and butadiene (combined) in a concentration of 0.1 to 30 wt.-%, more preferably 0. 5 to 25 wt.-% and most preferably 1 to 20 wt.-%. The stream S7 preferably comprises hydrogen in a concentration of 0.01 to 5 wt.-%, more preferably 0.02 to 2.5 Vol.-% and most preferably 0.05 to 2 wt.-%.In one aspect of the present invention, only a portion of medium boiling fraction S6, stream S6b is used as quench medium QM in step (iii). Accordingly, said medium boiling fraction S6 is separated in a splitting unit SPU into a first medium boiling fraction S6a and a second medium boiling fraction S6b. Said second medium boiling fraction S6b is then physically contacted as quench medium QM with the gaseous pyrolysis effluent S2 in the at least one quench unit QU and thereby separates said high boiling fraction S5 from said gaseous pyrolysis effluent S2 in the at least one quench unit QU in step (iii).The splitting unit SPU is selected from the group comprising or preferably consisting of tee, pipe(s) with associated valving, and combinations thereof, optionally further comprising a control system or control device for temperature and / or flow regulation.The weight ratio “S6a : S6b” preferably ranges from 0 to 1 , more preferably 0.1 to 0.8 and most preferably 0.2 to 0.6 to separate 20 to 70 wt.-%, more preferably 20 to 40 wt.-% of stream S2 in step (iv) as high boiling fraction S5, whereby a stream S9 having a final boiling point FBP in the range of 180 to 380, preferably 340 to 380 °C can be obtained in optional step (viii).Optionally, the first medium boiling fraction S6a and the low boiling fraction S8 are combined in a mixing unit MU to obtain a stream S9. Said stream S9 preferably has a final boiling point FPB (determined according to ASTM D86-23) of no more than 380 °C and is therefore suited as a feedstock or co-feedstock for a cracking process, preferably a steam cracking process in a steam cracking unit.Said first medium boiling fraction S6a and the low boiling fraction S8 can be combined in a mixing unit MU which be for example a tee or a storage facility such as a tank in which both streams are filled in.Optionally, said first medium boiling fraction S6a (in case not the whole medium boiling fraction S6 is used as quench medium QM in step (iii)), said low boiling fraction S8 or said stream S9 are then subjected to a steam cracking process as a feedstock or co-feedstock. Preferably, said stream(s) are upgraded by at least one upgrading process before fed into a steam cracking unit. Preferably, said at least upgrading process is selected from the group comprising washing, extraction, absorption, adsorption, distillation, hydrotreatment, catalytic cracking, catalytic aromatization, and combinations thereof. Such optional upgrading processes are for example described in WO 2021 / 224287 A1, WO 2023 / 061834 A1, EP 0713906 A1 and WO 95 / 03375 A1 . A skilled person knows how and in which cases to use upgrading processes disclosed in said documents and comparable upgrading processes disclosed elsewhere. Upgrading refers to e.g., reducing the oxygen, nitrogen and / or sulfur content of said stream(s), reducing the content of dienes comprised therein.Said stream(s) can also be co-feed with other feedstocks such as other pyrolysis oils, bio-naphtha and fossil feedstocks into a steam cracking unit.Steam cracking units suitable for the process according to the present invention are for example described in chapter H. Zimmermann, R. Walzl, Ullmanns Encyclopedia of Industrial Chemistry, Vol. 13, chapter “Ethylene”, sub-chapter “5.1.4 Commercial Cracking Ovens”, pages 482 to 490, 2012 Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim (DO 1 : 10.1002 / 14356007. a10_045. pub3) .The resulting olefins and aromatic hydrocarbons are important feedstocks for the chemical industry.Optionally, the process according to the present invention comprises the further step:converting at least one of the streams S5, S6a, S8, and / or optional stream S9 into a product PRF1.The product PRF1 is preferably selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orHi) industrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings poly isocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.The content of the at least one of the streams S5, S6a, S8, and / or optional stream S9 in the product PRF1 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 the content of the at least one of the streams S5, S6a, S8, and / or optional stream S9 in the product PRF1 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 the content is preferably 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 the International Sustainability and Carbon Certification (ISCC) standard.The publication Prior Art Disclosure; Issue 684; paragraphs

[1000] to

[8005] ; ISSN: 2198-4786; published: February 12, 2024 will be regarded as Reference RF1 , which is incorporated herein by reference in its entirety. Preferably, the product PRF1 is a product as described in Reference RF1 ; paragraphs

[1000] to

[8005] , Preferably, the process described herein is further a process to produce a product, preferably product PRF1.The converting step to obtain the product PRF1 preferably comprises one or more step(s) as described below and can be performed by conventional methods well known to a person skilled in the art. The converting step preferably comprises one or more step(s) selected from: recycling, preferably depolymerizing, gasifying, pyrolyzing, and / orsteam cracking; and / or purifying, preferably crystallizing, (solvent) extracting, distilling, evaporating, hydrotreating, absorbing, adsorbing and / or subjecting to ion exchanger; and / or assembling, preferably foaming, synthesizing, chemical conversion, chemically transforming, polymerizing and / or compounding; and / or forming, preferably foaming, extruding and / or molding; and / or finishing, preferably coating and / or smoothing. In addition, the one or more step(s) are described in detail in Reference RF1 ; paragraphs

[1000] to

[8005] ,The term “building block”, as used herein, comprises compounds, which are in a gaseous or liquid state under standard conditions of 0 °C and 0.1 MPa. Building blocks are typically used in chemical industry to form secondary products, which provide a higher structural complexity and / or higher molecular weight than the building block on which the secondary product is based. The building block is preferably selected from the group consisting of hydrogen, carbon monoxide, carbon dioxide, ethylene oxide, ethylene glycols, syngas comprising a mixture of hydrogen and carbon monoxide, alkanes, alkenes, alkynes and aromatic compounds. The alkanes, alkenes, alkynes and aromatic compounds comprise in particular 1 to 12 carbon atoms, respectively.The term “monomer”, as used herein, comprises molecules, which can react with each other to form polymer chains by polymerization. The monomer is preferably selected from the group consisting of (meth)acrylic acid, salts of (meth)acry I ic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Meth)acrylates comprising 1 to 22 carbon atoms are preferred, in particular comprising 1 to 8 carbon atoms. The terms (meth)acrylic acid, (meth)acrolein or (meth)acrylate relate to acrylic acid, acrolein or acrylate and also to methacrylic acid, methacrolein or methacrylate, where applicable. Further, the monomer can be selected from hexamethylenediamine (HMD) and adipic acid.The building block can further be an intermediate compound. The term “intermediate compound”, as used herein, comprises organic reagents, which are applied for formation of compounds with higher molecular complexity. The intermediate compound can be selected for example from the group consisting of phosgene, polyisocyanates and propylene oxide. The polyisocyanates are in particular aromatic di- and polyisocyanates, preferably toluene diisocyanate (TDI) and / or diphenylmethane diisocyanate (MDI). The building block and the monomer and typical converting step(s) to obtain the building block or monomer are described in more detail in paragraphs

[1000] to

[1012] of Reference RF1.The term “polymer A”, as used herein, comprises thermoplastic, e.g., polyamide or thermoplastic polyurethane, thermoset, e.g., polyurethane, elastomer, e.g., polybutadiene, or a copolymer or a mixture thereof and is defined in more detail in paragraphs

[2001] to

[2007] of Reference RF1 . The term “polymer composition A”, as used herein, comprises all compositions comprising a polymer as described above and one or more additive(s), e.g. reinforcement, colorant, modifier and / or flame retardant, and is defined in more detail in paragraph

[2008] of Reference RF1. The term “polymer product A”, as used herein, comprises any product comprising the polymer A and / or polymer composition A as described above and is defined in more detail in paragraphs

[2009] and

[2010] of Reference RF1. The step(s) to obtain the polymer, preferably polymer A, polymer composition, preferably polymercomposition A or polymer product, preferably polymer product A is / are described in more detail in paragraph

[2011] of Reference RF1.The term “industrial use polymer'1, as used herein, comprises rheology, polycarboxylate, alkoxylated polyalkylenamine, alkoxylated polyalkylenimine, polyether-based, dye inhibition and soil release cleaning polymers defined in more detail in paragraphs

[3035] to

[3044] of Reference RF1. The term “industrial use surfactant”, as used herein, comprises non-ionic, anionic and amphoteric industrial use surfactants defined in more detail in paragraphs

[3008] to

[3034] of Reference RF1. The term “industrial use descaling compound”, as used herein, comprises non- phosphate-based builders (NPB) and phosphonates (CoP) described in more detail in paragraphs

[3001] to

[3005] of Reference RF1. The term “industrial use biocide”, as used herein, refers to a chemical compound that kills microorganisms or inhibits their growth or reproduction defined in more detail in paragraphs

[3006] to

[3007] of Reference RF1. The term “industrial use solvent”, as used herein, comprises alkyl amides, alkyl lactamides, alkyl esters, lactate esters, alkyl diester, cyclic alkyl diester, cyclic carbonates, aromatic aldehydes and aromatic esters defined in more detail in paragraphs

[3045] to

[3055] of Reference RF1. The term “industrial use dispersant1, as used herein, comprises anionic and non-ionic industrial use dispersants defined in more detail in paragraphs

[3056] to

[3058] of Reference RF1. The term “composition and / or formulation thereof” with reference to the industrial use polymers, industrial use surfactants, descaling compounds and / or industrial use biocides refers to industrial use compositions and / or institutional use products and / or fabric and home care products and / or personal care products defined in more detail in paragraph

[3059] of Reference RF1. The converting step(s) to obtain the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3060] of Reference RF1. The converting steps to obtain the industrial use composition or formulation of the industrial use polymer, industrial use surfactant, descaling compound and / or industrial use biocide are defined in more detail in paragraph

[3061] of Reference RF1.The term “agrochemical composition”, as used herein, typically relates to a composition comprising an agrochemically active ingredient and at least one agrochemical formulation auxiliary. Examples of agrochemical compositions, active ingredients and auxiliaries are described in more detail in Reference RF1, paragraph

[4001] , The agrochemical composition may take the form of any customary formulation. The agrochemical compositions are prepared in a known manner, e.g. described by Mollet and Grubemann, Formulation technology, Wiley VCH, Weinheim, 2001 ; or Knowles, New developments in crop protection product formulation, Agrow Reports DS243, T&F Informa, London, 2005. The converting step(s) to obtain the agrochemically active ingredients and auxiliaries may be conducted in analogy to the production step(s) of their analogues that are based on petrochemicals or other precursors that are not gained by recycling processes. In addition, conversion to compounds mentioned in sections “Polymer'1and “Cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or compositions or formulations thereof” may be performed as described in these sections as well as the respective paragraphs in Reference RF1.The term active pharmaceutical ingredients and / or intermediates thereof, as used herein, comprises substances that provide pharmacological activity or other direct effect in the diagnosis, cure, mitigation, treatment, or prevention of disease, or to affect the structure or any function of the body. Intermediates thereof are isolated products that are generated during a multi-step route of synthesis of an active pharmaceutical ingredient. The term pharmaceutical excipients, as used herein, comprises compounds or compound mixtures used in compositions for various pharmaceutical applications, which are not substantially pharmaceutically active on itself. Active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients are defined in more detail in paragraph

[5001] of Reference RF1. The converting step(s) to obtain the active pharmaceutical ingredients and / or intermediates thereof and pharmaceutical excipients may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms animal feed additives, human food additives, dietary supplements, as used herein, comprises Vitamins, Pro-Vitamins and active metabolites thereof including intermediates and precursors, especially Vitamin A, B, E, D, K and esters thereof, like acetate, propionate, palmitate esters or alcohols thereof like retinol or salts thereof and any combinations thereof; Tetraterpenes, especially isoprenoids like carotenoids and xanthophylls including their intermediates and precursors as well as mixtures and derivates thereof, especially beta carotene, Canthaxanthin, Citranaxanthin, Astaxanthin, Zeaxanthin, Lutein, Lycopene, Apo-carotenoids, and any combinations thereof; organic acids, especially formic acid, propionic acid and salts thereof, such as sodium, calcium or ammonium salts, and any combinations thereof, such as but not limited to mixtures of formic acid and sodium formiate, propionic acid and ammonium propionate, formic acid and propionic acid, formic acid and sodium formiate and propionic acid, propionic acid and sodium propionate and formic acid and sodium formiate; glycerides of carboxylic acids and short and medium chain fatty acids, conjugated linoleic acids, such as omega-6 fatty acid (C18:2) methyl ester and 1 ,2- propandiol and beverage stabilizers, such as polyvinylpyrrolidone-polymer or polyvinyl i m idazole / polyvi nylpyrrol idone- copolymer. Animal feed additives, human food additives and dietary supplements are defined in more detail in paragraph

[5002] of Reference RF1. The converting step(s) to obtain the animal feed additives, human food additives, dietary supplements may comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The terms aroma chemical and aroma composition as used herein, comprise a volatile organic substance with a molecular weight between 70-250 g / mol comprising a functional group with a carbon skeleton of C5-C16 carbon atoms comprising linear, branched, cyclic, for example with a ring size of C5-C18, bicyclic or tricyclic aliphatic chains and but not necessarily one or more unsaturated structural elements like double bonds, triple bonds, aromatics or heteroaromatics and preferably the one or more additional functional groups are selected from alcohol, ether, ester, ketone, aldehyde, acetal, carboxylic acid, nitrile, thiol, amine. In one aspect, the aroma chemical is a terpene-based aroma chemical, for example selected from monoterpenes and monoterpenoids, sesquiterpenes and sesquiterpenoids, diterpenes, triterpenes or tetraterpenes. Aroma chemicals can be combined with further aroma chemicals to give an aroma composition. Aroma chemicals and aroma compositions are defined in more detail in paragraph

[5003] of Reference RF1. The converting step(s) to obtain the aroma chemical and aroma compositionmay comprise one or more synthesis steps and can be performed by conventional synthesis and techniques well known to a person skilled in the art.The term “aqueous polymer dispersion”, as used herein, comprises aqueous composition(s) comprising dispersed polymer(s) and is defined in more detail in the section

[6001] entitled “aqueous polymer dispersion” of Reference RF1 . The dispersed polymer(s) may be selected from acrylic emulsion polymer(s), styrene acrylic emulsion polymer(s), styrene butadiene dispersion(s), aqueous dispersion(s) comprising composite particles, acrylate alkyd hybrid dispersion(s), polyurethane(s) (including UV-curable polyurethanes) and polyurethane - poly(meth)acrylate hybrid polymer(s). The term “emulsion polymer”, as used herein, comprises polymer(s) made by free-radical emulsion polymerization. Aqueous polyurethane dispersion(s) are defined in more detail in the section

[6002] entitled “Polyurethane dispersions” of Reference RF1. UV-curable polyurethane(s) is / are defined in more detail in the section

[6017] of Reference RF1. Polyurethane - poly(meth)acrylate hybrid polymer(s) is / are defined in more detail in the section

[6016] of Reference RF1.The term “polymeric dispersant”, as used herein, comprises preferably polymer(s) comprising polyether side chain, in particular polycarboxylate ether polymer(s) and polycondensation product(s) defined in more detail in paragraph

[6020] entitled “Polymeric dispersant” of Reference RF1. The converting (polymerization) step(s) to obtain the aqueous polymer dispersion(s) comprising emulsion polymer(s) is / are defined in more detail in the section

[6003] entitled “Emulsion polymerization” of Reference RF1. The converting (polymerization) step(s) to obtain the aqueous polyurethane dispersion(s) is / are defined in more detail in the section

[6014] entitled “Process for the preparation of aqueous polyurethane dispersions” and section

[6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them” of Reference RF1 . Composition(s) and uses of aqueous polymer dispersion(s) and of polymeric dispersant(s) are defined in more detail in the following sections of Reference RF1 : section

[6004] entitled “Uses of aqueous polymer dispersions”, section

[6005] entitled “Binders for architectural and construction coatings”, section

[6006] entitled “Binders for paper coating”, section

[6007] entitled “Binders for fiber bonding”, section

[6008] entitled “Adhesive polymers and adhesive compositions”, section

[6015] entitled “Aqueous polyurethane dispersions suitable for use in coating compositions”, section

[6016] entitled “Aqueous polyurethane - poly(meth)acrylate hybride polymer dispersions suitable for use in coating compositions”, section

[6017] entitled “Aqueous UV-curable polyurethane dispersions, their preparation and use and compositions containing them”, section

[6018] entitled “Inorganic binder compositions comprising polymeric dispersants and their use”

[6019] 100% curable coating compositions, UV-crosslinkable poly(meth)acrylate(s) and its / their uses are defined in more detail in section

[6009] entitled “UV-crosslinkable poly(meth)acrylates for use in UV-curable solvent- free hotmelt adhesives and their use for making pressure-sensitive self-adhesive articles” of Reference RF1.Polyisocyanate(s), composition(s) comprising them and their uses are defined in more detail in section

[6010] entitled “Polyisocyanates” of Reference RF1.Hyperbranched polyester polyol(s) and its / their uses are defined in more detail in section

[6011] entitled “Organic solvent based hyperbranched polyester polyols suitable for use in coating compositions” of Reference RF1 . The converting step(s) to obtain the hyperbranched polyester polyols is / are defined in more detail in the section

[6012] entitled “Preparation of organic solvent based hyperbranched polyester polyols” of Reference RF1. Coating composition(s) comprising hyperbranched polyester polyol(s), polyisocyanate(s) and additive(s) and substrate(s) coated therewith are defined in more detail in section

[6013] entitled “Organic solvent based two component coating compositions comprising hyperbranched polyester polyols and polyisocyanates” of Reference RF1 .Unsaturated polyester polyol(s), solvent-based coating composition(s) comprising said unsaturated polyester polyol(s) and substrate(s) for coating with said coating composition(s) are defined in more detail in section

[6018] entitled “Organic solvent-based coating composition comprising unsaturated polyester polyols” of Reference RF1. 100% curable coating composition(s) is / are defined in more detail in section

[6019] of Reference RF1.Polymeric dispersant(s) for inorganic binder compositions is / are defined in more detail in section

[6020] of Reference RF1 . The inorganic binder composition(s) comprising the polymeric dispersants and their use are defined in more detail in section

[6021] of Reference RF1. The converting step(s) to obtain the polymeric dispersant(s) are defined in more detail in section

[6020] of Reference RF1 . The term “inorganic binder composition” comprising the polymeric dispersant(s), as used herein, comprises preferably in particular hydraulically setting compositions and compositions comprising calcium sulfate and is defined in more detail in section

[6021] of Reference RF1 entitled “Inorganic binder compositions comprising the polymeric dispersant and their use”. Specific building material formulation(s) comprising polymeric dispersant(s) or building product(s) produced by a building material formulation comprising a polymeric dispersant are disclosed in more detail in section

[6021] of Reference RF1 .The term “cosmetic surfactant”, as used herein, comprises non-ionic, anionic, cationic and amphoteric surfactants and is defined in more detail in paragraph

[7002] of Reference RF1 . The term “emollient”, as used herein, refers to a chemical compound used for protecting, moisturizing, and / or lubricating the skin and is defined in more detail in paragraph

[7003] of Reference RF1. The term “wax”, as used herein, comprises pearlizers and opacifiers and is defined in more detail in paragraph

[7004] of Reference RF1. The term “cosmetic polymer”, as used herein, comprises any polymer that can be used as an ingredient in a cosmetic formulation and is defined in more detail in paragraph

[7005] of Reference RF1. The term “UV filter”, as used herein, refers to a chemical compound that blocks or absorbs ultraviolet light and is defined in more detail in paragraph

[7006] of Reference RF1. The term “further cosmetic ingredient”, as used herein, comprises any ingredient suitable for making a cosmetic formulation. Several sources disclose cosmetically acceptable ingredients. E. g. the database Cosing on the internet pages of the European Commission discloses cosmetic ingredients and the International Cosmetic Ingredient Dictionary and Handbook, edited by the Personal Care Products Council (PCPC), discloses cosmetic ingredients. The term “composition and / or formulation thereof’ with reference to the cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter and / or further cosmetic ingredient refers to personal care and / or cosmetic compositions or formulations defined in more detail in paragraph

[7007] of Reference RF1 . The converting step(s) to obtain the cosmeticsurfactant, emollient, wax, cosmetic polymer, UV filter or further cosmetic ingredient is / are defined in more detail in paragraph

[7008] of Reference RF1.The terms “polymer B”, “polymer composition B”, “coating composition”, “other functional composition”, “foil”, “molded body”, “coating” and “coated substrate” are well known to the person skilled in the art and are defined in more detail from paragraph

[8000] to

[8005] of Reference RF1.The present invention further concerns a pyrolysis plant which is suited for the process according to the present invention. The pyrolysis plant for separating a high boiling fraction from a plastic waste pyrolysis effluent comprises a) at least one pyrolysis unit PU, b) at least one quench unit QU, wherein said at least one quench unit QU is downstream of and fluidically connected to said at least one pyrolysis unit PU and wherein the quench medium comprises or preferably consists of the medium boiling fraction S8b, c) at least one separation unit SU, wherein said at least one separation unit SU is downstream of and fluidically connected to said at least one quench unit QU, d) at least one first condensation unit CU1 , wherein said at least one first condensation unit CU1 is downstream of and fluidically connected to said at least one separation unit SU, e) at least one second condensation unit CU2, wherein said at least one second condensation unit CU2 is downstream of and fluidically connected to said at least one first condensation unit CU1 , f) at least one splitting unit SPU, wherein said at least one splitting unit SPU is downstream of and fluidically connected to said at least one first condensation unit CU1, and g) optionally at least one mixing unit MU, wherein said at least one mixing unit is downstream of and fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2.The at least one pyrolysis unit PU preferably comprises a reactor chamber and a rotation mechanism, wherein said pyrolysis unit PU is preferably a pyrolysis unit PU1 or a pyrolysis unit PU2. Said rotation mechanism is preferably selected from the group comprising or preferably consisting of conveyor screws, conveyor double screws, fluidization units, preferably radially extending fluidization units, and combinations thereof. Said at least one quench unit QU is preferably selected from the group comprising or preferably consisting of tangential-injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of said second medium boiling fraction S6b, and counter-flow washers. Said separation unit SU is selected from the group comprising or preferably consisting of gravity separators, centrifugal separators, filter vane separators, liqu id / gas coalescers, and combinations thereof. Said first condensation unit CU1 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense, and combinations thereof. Said optional the splitting unit SPU is selected from the group comprising or preferably consisting of tee, pipe(s) with associated valving, and combinations thereof. Said second condensation unit CU2 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense, and combinations thereof.The present invention is further illustrated by the following set of embodiments and combinations of embodiments resulting from the dependencies and back-references as indicated. In particular, it is noted that in each instance where a range of embodiments is mentioned, for example in the context of a term such as "The process of any of embodiments 1 to 3", every embodiment in this range is meant to be explicitly disclosed for the skilled person, i.e. the wording of this term is to be understood by the skilled person as being synonymous to "the process of any of embodiments 1 , 2 and 3". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and thus, suitably supports the claims of the present invention.1 . Process for separating a high boiling fraction from a plastic waste pyrolysis effluent, said process comprising the steps(i) providing a feed stream S1 , wherein said feed stream S1 comprises or preferably consists of plastic waste,(ii) converting said feed stream S1 by pyrolysis in at least one pyrolysis unit PU into a solid residue S3 and a gaseous pyrolysis effluent S2, wherein said gaseous pyrolysis effluent S2 comprises a high boiling fraction S5, a medium boiling fraction S6, a low boiling fraction S8, a non-condensable stream S7 and optionally water,(iii) quenching said gaseous pyrolysis effluent S2 in at least one quench unit QU with a quench medium QM and thereby forming a first intermediate stream S4, wherein said gaseous pyrolysis effluent S2 and said quench medium QM are physically contacted in the at least one quench unit QU, and wherein said first intermediate stream S4 comprises a liquid and a gaseous phase, wherein said quench medium QM is selected from the group comprising or preferably consisting of second medium boiling fraction S6b optionally separated in step (vii), medium boiling fraction S6 condensed and separated in step (v), mixtures thereof, and mixtures thereof further comprising at least one further oil FO, wherein said first intermediate stream S4 has a temperature of 180 to 350 °C when leaving the at least one quench unit QU,(iv) separating said liquid and a gaseous phase comprised in said first intermediate stream S4, wherein said liquid phase comprises or consists of said high boiling fraction S5, and wherein said gaseous phase comprises or consists of a second gaseous intermediate stream S4',(v) condensing and separating a fraction of said second gaseous intermediate stream S4' in a first condensation unit CU1, wherein said condensed and separated fraction comprises or consists of said medium boiling fraction S6, and wherein the remaining gaseous fraction of said second gaseous intermediate stream S4' comprises or consists of a third gaseous intermediate stream S4",(vi) condensing and separating a fraction of said third intermediate stream S4" in a second condensation unit CU2, wherein said condensed and separated fraction comprises or consists of said low boiling fraction S8 and optionally water, and wherein and the remaining gaseous fraction of said third gaseous intermediate stream S4" comprises or consists of said non-condensable stream S7,(vii) optionally dividing said medium boiling fraction S6 in a splitting unit SPU into at least two portions, wherein the first portion is a first medium boiling fraction S6a, wherein the second portion is a second medium boiling fraction S6b, and wherein said second medium boiling fraction S6b is physically contacted in step (iii) as quench medium QM with the gaseous pyrolysis effluent S2 in the at least one quench unit QU, and(viii) optionally combining the first medium boiling fraction S6a and the low boiling fraction S8 in a mixing unit MU to obtain a stream S9. Process according to embodiment 1 wherein the feed stream S1 comprises at least one polymer selected from the group comprising or consisting of polyolefins, polystyrene, copolymers comprising styrene units, polyvinylchloride, polyvinylidene chloride, polyamides, polyurethanes, polyesters, polycarbonate, polyesters, rubbers, and mixtures thereof. Process according to embodiment 1 or 2 wherein 20 to 70 wt.-%, preferably 20 to 40 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom. Process according to any one of embodiments 1 to 3 wherein said gaseous pyrolysis effluent S2 has a temperature of preferably 250 to 900 °C, more preferably 300 to 700 °C and most preferably 350 to 550 °C when entering the at least one quench unit QU. Process according to any one of embodiments 1 to 4 wherein said first intermediate stream S4 has a temperature of 200 to 280 °C and preferably 230 to 270 °C when leaving the at least one quench unit QU. Process according to any one of embodiments 1 to 5 wherein the at least one quench unit QU is selected from the group comprising or preferably consisting of tangential-injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of the quench medium QM, and counter-flow washers. Process according to any one of embodiments 1 to 6 wherein the separation unit SU is selected from the group comprising or preferably consisting of gravity separators, centrifugal separators, filter vane separators, liquid / gas coalescers, and combinations thereof. Process according to any one of embodiments 1 to 7 wherein the high boiling fraction S5 comprises C 11 -C21 + hydrocarbons. Process according to any one of embodiments 1 to 8 wherein the high boiling fraction S5 has an initial boiling point IBP (determined according to ASTM D86-23) of more than 170 °C, preferably of more than 180 °C and more preferably of more than 190 °C.10. Process according to any one of embodiments 1 to 9 wherein the further oil FO is selected from the group comprising or preferably consisting of pyrolysis oils not formed by the process according to the present invention, the pyrolysis fuel oil fraction formed by steam cracking of hydrocarbons, fresh mineral lubricating oils, used mineral lubricating oils, bio-oils, oils formed by fluid catalytic cracking, oils formed by hydrocracking and combinations thereof.11. Process according to any one of embodiments 1 to 9 wherein the quench medium QM consists of one member selected from the group consisting of the liquid second medium boiling fraction S6b, the liquid medium boiling fraction S6, mixtures thereof, and mixtures thereof further comprising at least one further oil FO.12. Process according to any one of embodiments 1 to 10 wherein at least a portion of the high boiling fraction S5 is subjected as a feedstock or co-feedstock to a process selected from the group comprising or preferably consisting of partial oxidation, fluid catalytic cracking, hydrocracking, coking, visbreaking and other refining processes.13. Process according to any one of embodiments 1 to 11 wherein said second intermediate stream S4' is depleted in C11-C21 + hydrocarbons compared to said first intermediate stream S4.14. Process according to any one of embodiments 1 to 12 wherein the first condensation unit CU1 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense, and combinations thereof.15. Process according to any one of embodiments 1 to 13 wherein said medium boiling fraction S6 comprises C6-C20 hydrocarbons.16. Process according to any one of embodiments 1 to 14 wherein said medium boiling fraction S6 has a final boiling point FBP (determined according to ASTM D86-23) of preferably less than 400 °C, more preferably less than 380 °C and most preferably 370 °C.17. Process according to any one of embodiments 1 to 15 wherein the medium boiling fraction S6 has a D86- 50 % value (determined according to ASTM D86-23) of more than 200 °C, preferably of more than 210 °C and more preferably of more than 225 °C.18. Process according to any one of embodiments 1 to 17 wherein the optional splitting unit SPU is selected from the group comprising or preferably consisting of tee, pipe(s) with associated valving, and combinations thereof.19. Process according to any one of embodiments 1 to 18 wherein the weight ratio “S6a : S6b” preferably ranges from 0 to 1 , more preferably 0.1 to 0.8 and most preferably 0.2 to 0.6.20. Process according to any one of embodiments 1 to 19 wherein the temperature of the quench medium QM when physically contacted with said gaseous pyrolysis effluent S2 in the at least one quench unit QU preferably ranges from 10 to 200 °C, more preferably 50 to 150 °C and most preferably 80 to 120 °C.21. Process according to any one of embodiments 1 to 19 wherein said second condensation unit CU2 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense, and combinations thereof.22. Process according to any one of embodiments 1 to 20 wherein said low boiling fraction S8 comprises C6-C10 hydrocarbons.23. Process according to any one of embodiments 1 to 21 wherein said low boiling fraction S8 has a final boiling point FBP (determined according to ASTM D86-23) of preferably less than 230 °C, more preferably less than 220 °C and most preferably 210 °C.24. Process according to any one of embodiments 1 to 23 wherein a water stream S10 is separated from the third intermediate stream S4" in the second condensation unit CU2.25. Process according to any one of embodiments 1 to 24 wherein said non-condensable stream S7 comprises C1 -C5 hydrocarbons.26. Process according to any one of embodiments 1 to 24 wherein said at least one pyrolysis unit PU comprises a reactor chamber and a rotation mechanism, wherein said pyrolysis unit PU is preferably a pyrolysis unit PU1 or a pyrolysis unit PU2.27. Process according to embodiment 26 wherein said rotation mechanism is selected from the group comprising or preferably consisting of conveyor screws, conveyor double screws, fluidization units, preferably radially extending fluidization units, and combinations thereof.28. Process according to embodiment 27 wherein the peripheral speed of the extending fluidization units during operation of the pyrolysis unit PU1 preferably ranges from 15 to 135 m / s, more preferably from 35 to 85 m / s.29. Process according to embodiment 26 wherein the residence time for the feed stream S1 inside the pyrolysis unit PU2 preferably range from 2.5 to 40 min.30. Process according to any one of embodiments 1 to 29 wherein the at least one quench unit QU has at least a first inlet 11 and a second inlet I2, and at least a first outlet 01 , wherein said gaseous pyrolysis effluent S2 enters the at least one quench unit QU through said first inlet 11, said second medium boiling fraction S6b or said medium boiling fraction S6 enters the at least one quench unit QU through said second inlet I2 and wherein said first intermediate stream S4 leaves the at least one quench unit QU through said first outlet 01.31. Process according to any one of embodiments 1 to 30 wherein said separation unit SU has at least a first inlet 1'1 and at least a first outlet 0'1 and at least a second outlet 0'2, wherein said first intermediate stream S4 enters said separation unit SU through said at least one first inlet 1'1 , said high boiling fraction S5 leaves said separation unit through said at least one first outlet 0'1 and said second intermediate stream S4' leaves said separation unit SU through said at least one second outlet 0'2.32. Process according to any one of embodiments 1 to 31 wherein the at least one quench unit QU and said separation unit SU are combined in a quench and separation unit QSU.33. Process according to any one of embodiments 1 to 32 wherein the splitting unit SPU is selected from the group comprising or preferably consisting of tee, pipe(s) with associated valving, and combinations thereof, optionally further comprising a control system or control device for temperature and / or flow regulation.34. Process according to any one of embodiments 1 to 33, comprising steps (i) to (viii) and further comprising step (ix): feeding at least a portion of stream S9 into a steam cracking unit.35. Pyrolysis plant for separating a high boiling fraction from a plastic waste pyrolysis effluent comprising a) at least one pyrolysis unit PU, b) at least one quench unit QU, wherein said at least one quench unit QU is downstream of and fluidically connected to said at least one pyrolysis unit PU, c) at least one separation unit SU, wherein said at least one separation unit SU is downstream of and fluidically connected to said at least one quench unit QU, wherein the quench medium comprises or preferably consists of the medium boiling fraction S6b, d) at least one first condensation unit CU1, wherein said at least one first condensation unit CU1 is downstream of and fluidically connected to said at least one separation unit SU, e) at least one second condensation unit CU2, wherein said at least one second condensation unit CU2 is downstream of and fluidically connected to said at least one first condensation unit CU1, f) optionally at least one splitting unit SPU, wherein said at least one splitting unit SPU is downstream of and fluidically connected to said at least one first condensation unit CU1, andg) optionally at least one mixing unit MU, wherein said at least one mixing unit is downstream of and fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2.36. Pyrolysis plant according to embodiment 35 wherein the at least one pyrolysis unit PU comprises a reactor chamber and a rotation mechanism, wherein said pyrolysis unit PU is preferably a pyrolysis unit PU1 or a pyrolysis unit PU2.37. Pyrolysis plant according to embodiment 36 wherein said rotation mechanism is selected from the group comprising or preferably consisting of conveyor screws, conveyor double screws, fluidization units, preferably radially extending fluidization units, and combinations thereof.38. Pyrolysis plant according to any one of embodiments 35 to 37 wherein the at least one quench unit QU is selected from the group comprising or preferably consisting of tangential-injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of said second medium boiling fraction S6b, and counter-flow washers.39. Pyrolysis plant according to any one of embodiments 34 to 37 wherein the separation unit SU is selected from the group comprising or preferably consisting of gravity separators, centrifugal separators, filter vane separators, liquid / gas coalescers, and combinations thereof.40. Pyrolysis plant according to any one of embodiments 35 to 39 wherein the first condensation unit CU 1 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense, and combinations thereof.41. Pyrolysis plant according to any one of embodiments 35 to 40 wherein optional the splitting unit SPU is selected from the group comprising or preferably consisting of tee, pipe(s) with associated valving, and combinations thereof.42. Pyrolysis plant according to any one of embodiments 35 to 41 wherein the second condensation unit CU2 is selected from the group comprising or preferably consisting of flash drums, strippers, distillation columns, quench columns, heat exchangers with cooled surfaces to condense, and combinations thereof.43. Use of the pyrolysis plant according to any one of embodiments 35 to 42 for the process according to any one or embodiments 1 to 34.The invention will be further explained by the following non-limiting examples.ExamplesThe process according to the present invention (Examples 1 to 4) and comparative examples were simulated using ASPEN Plus™ V14 simulation software. The assumptions and results for steps (i) (feed stream S1) and (ii) (conversion of the feed stream S1 in a pyrolysis unit PU by pyrolysis into a gaseous pyrolysis effluent S2) were kept constant for all examples including the comparative examples: A feed stream S1 was converted into a gaseous pyrolysis effluent S2 in a pyrolysis unit PU. The solid residue S3 contains the coke formed during the pyrolysis reaction, optionally other inorganic solids such as fillers, and optionally added solid pyrolysis catalyst particles. The solid residue S3 was removed in the pyrolysis unit PU. The temperature, pressure, mass flow and mass fractions (given in wt.-%) of feed stream S1 and the resulting gaseous pyrolysis effluent S2 and solid residue S3 were kept constant throughout all examples and are summarized in T able 1 .T able 1 : parameters used for streams S 1 , S2 and S3 throughout all examples (including comparative examples).S1 S2 S3T [°C] 25 500 25P [bar ( 1.2 1.2 1.2Total m 1020 1000 20Mole va 0 1 0H2[wt- 0.03CO [wt.- 0.26CO2[wt. 1.22H2O [wt. 2.7CH4[wt. 0.97C2-C5 10.83C6-C10 25.92C11-C2 38.85C21+ [w 17.03HA" [wt 2.18 0“solids” 100 plastic w 100 provided*“mole vapor-frac” corresponds to the molar frac ion of gaseous components in the corresponding stream Sn (0=liquid; 1 =gas)"HA = components comprising at least one heteroatom”, such as nitriles (benzonitrile for example), primary amines (aniline for example), e- caprolactam, chinolines (dimethylchinoli ne for example) for components comprising N; thiophenes (benzothiophen for example) for components comprising S; methylbenzothiazol (for example) for components comprising N and S; carboxylic acids (benzoic acid, terephthalic acid for example), alcohols, (iso-nonanol for example) for components comprising 0.Example 1The target product is a stream S9 having a final boiling point FBP (D86-100%) (determined according to ASTM-D86- 23) of 380 °C. Such a stream S9 is suited as a feedstock for producing C2-C4 olefins and C6-C8 aromatic hydrocarbons by steam cracking.In the next step, the gaseous pyrolysis effluent S2 was mixed with second medium boiling fraction S6b (Tab. 2) whereby the high boiling fraction S5 was condensed from the gaseous pyrolysis effluent S2. The temperature of the second medium boiling fraction S6b was 97 °C. With a mass-ratio (stream S6b : S2) of 1.016 : 1 the first intermediate stream S4 had a molar vapor faction of 0.957 and a temperature of 267.1 °C. In the separation unit SU, the high boiling fraction S5 was 20.8 % of the gaseous pyrolysis effluent S2. In this high boiling fraction S5 the high boiling hydrocarbons C21 + were accumulated with 63.74 wt.-%. This was also shown by the initial boiling point D86- 0% of 191 °C and the final boiling point D86-100% of 556 °C.The first condensation unit CU1 was operated at 97 °C and 1.15 bar(abs.). In this first condensation unit CU1 the medium boiling fraction S6 was condensed from the gaseous second intermediate stream S4'. In this medium boiling fraction S6 the high boiling hydrocarbons C21+ are reduced to 6.92 wt.-%. This was also shown by the initial boiling point D86.0% of 81 °C and the final boiling point D86-100% of 386 °C. The residual water content in the medium boiling fraction S6 was only 0.06 wt.-%. Hence, no separate liquid water phase was built.A portion of said medium boiling fraction S6, namely the second medium boiling fraction S6b was used for quenching the gaseous pyrolysis effluent S2 in the quench unit QU. The amount of required second medium boiling fraction S6b was fed to the quench unit QU. This amount is composed of 1) the desired final boiling point D86-100 % of stream S9, 2) the temperature and flow rate of the gaseous pyrolysis effluent S2 before entering the quenching unit QU and 3) the temperature and flow rate of the second medium boiling fraction S6b before entering the quenching unit QU.Portions of the third intermediate stream S4"were then condensed in the second condensation unit CU2. The condensation unit CU2 was operated at 25 °C and 1 .1 bar(abs.). Under these conditions, the vapor phase from the second condensation unit CU2, the gas stream S7 contained the permanent gases and the non-condensed hydrocarbons with 71.86 wt.-% C2-C5 and 4.15 wt.-% C6-C10. The liquid phase condensed in the second condensation unit CU2 consisted of a water phase stream S10 and the low boiling fraction S8 which separated from each other because of insufficient miscibility. The water phase stream S10 was withdrawn from the process. The water phase stream S10 contained water soluble components comprising hetero atoms which were formed by the pyrolysis reaction. The low boiling fraction S8 contained 63.22 wt.-% C6-C10 hydrocarbons and only 4.3 wt.-% C11-C20 hydrocarbons. The resulting initial boiling point D86-0% of the low boiling fraction S8 was -24 °C and the final boiling point D86-100% was 199 °C.The first medium boiling fraction S6a was combined with the low boiling fraction S8 to obtain the stream S9 in a mixing unit MU. Stream S9 comprised 49 wt.-% C11-C20 hydrocarbons and only 5.79 wt.-% C21 + hydrocarbons. The resulting initial boiling point D86-0% of stream S9 was 15 °C and the desired final boiling point D86-100% 380 °C. Stream S9 was suited as a feedstock for a cracking unit such as a steam cracking unit. Taking also into account the gas stream S7, the yield of the valued product (yield stream S7 and yield stream S9 combined), was 79 %. The respective mass fractions are given in wt.-%.Table 2: results from example 1 .S4 S5 S6a S6b S7 S8 S9 S10T [°C] 267.1 267.1 97 97 25 25 25 25 p [bar (abs.)]1.2 1.2 1.2 1.2 1.1 1.1 3 3Total mass flow [kg / h] 2016 208 542 1016 121 106 648 23Mole vapor frac 0.957 0 0 0 1 0 0 0H2[wt.-%] 0.02 0 0 0 0.27 0 0 0CO [wt.-%] 0.13 0 0 0 2.15 0 0 0CO2[wt.-%] 0.61 0 0.01 0.01 9.97 0.1 0.02 0.03H2O [wt.-%] I .37 0 0.06 0.06 3.38 0.03 0.06 97.4CH4[wt.-%] 0.48 0 0 0 8.05 0.02 0 0C2-C5 [wt-%] 5.7 0.02 0.66 0.66 71.86 17.08 3.34 0.01C6-C10 [wt.-%] 28.64 1.38 31.32 31.32 4.15 77.05 38.79 0.01C11-C20 [wt-%] 48.27 34.1 57.54 57.54 0.01 5.24 49 0C21 + [wt-%] I I .94 63.74 6.92 6.92 0 0 5.79 0HA [wt-%] 2.84 0.76 3.49 3.49 0.15 0.48 3 2.55D86-0 %1[°C] 191 81 81 - -21 15D86-50 % [°C] 366 230 230 - 125 206D86-100 %2[°C] 556 386 386 - 206 3801D86-0 % = IBP2D86-100 % = FBPStream S9 has a final boiling point of 380 °C and, accordingly, is suited as a feedstock for a steam cracking process. Said desired final boiling point FPB of stream S9 was reached by separating 20.8 wt-% of stream S2 (calculated from total mass flow S2 = 1000 kg / h (Table 1) and total mass flow S5 = 208 kg / h (Table 2)) in step (iv) as high boiling fraction S5 from the gaseous pyrolysis effluent S2. Said process is less energy consuming than processes known from prior art because no additional process step such as distillation is required to produce a pyrolysis oil fraction which is suited as feedstock for a steam cracking process. Example 2The target product is a stream S9 having a final boiling point FBP (determined according to ASTM-D86-23) of 360 °C. Such a stream S9 is suited as a feedstock for producing C2-C4 olefins and C6-C8 aromatic hydrocarbons by steam cracking. The respective mass fractions are given in wt-%.Table 3: results from example 2.S4 S5 S6a S6b S7 S8 S9 S10T [°C] 255.4 255.4 97 97 25 25 25 25 p [bar (abs.)] 1.2 1.2 1.2 1.2 1.1 1.1 3 3Total mass flo 2129.1 270 475 1129 121 111 586 23Mole vapor-fra 0.944 0 0 0 1 0 0 0H2[wt.-%] 0.02 0 0 0 0.27 0 0 0CO [wt.-%] 0.12 0 0 0 2.14 0 0 0CO2[wt.-%] 0.57 0 0.01 0.01 9.94 0.10 0.02 0.03H2O [wt.-%] 1.3 0 0.06 0.06 3.56 0.03 0.06 97.4CH4[wt-%] 0.46 0 0 0 8.03 0.02 0 0C2-C5 [wt-% 5.45 0.02 0.69 71.68 17.08 3.34 0.01C6-C10 [wt.- 30.4 1.89 34.36 34.36 4.22 77.05 38.79 0.01C11-C20 [wt- 48.41 41.6 56.88 56.88 0.01 5.24 49 0C21+ [wt-%] 10.28 55.41 4.3 4.3 0 0 5.79 0HA [wt-%] 2.98 1.07 3.7 3.7 0.15 0.48 3 2.55D86-0 % [°C] 185 82 - -21 15D86-50 % [°C 354 216 - 125 194D86-100 % [° 547 366 - 205 360Stream S9 has a final boiling point of 360 °C and, accordingly, is suited as a feedstock for a steam cracking process.Said desired final boiling point FPB of stream S9 was reached by separating 27 wt-% of stream S2 (calculated from total mass flow S2 = 1000 kg / h (T able 1 ) and total mass flow S5 = 270 kg / h (T able 3)) in step (iv) as high boiling fraction S5 from the gaseous pyrolysis effluent S2. Said process is less energy consuming than processes known from prior art because no additional process step such as distillation is required to produce a pyrolysis oil fraction which is suited as feedstock for a steam cracking process. Example 3The target product is a stream S9 having a final boiling point FBP (determined according to ASTM-D86-23) of340 °C. Such a stream S9 is suited as a feedstock for producing C2-C4 olefins and C6-C8 aromatic hydrocarbons by steam cracking. The respective mass fractions are given in wt-%.Table 4: results from example 3.S4 S5 S6a S6b S7 S8 S9 S10T [°C] 239.2 239.2 97 97 25 25 25 25P [bar (abs.)] 1.2 1.2 1.2 1.2 1.1 1.1 3 3Total mass flo 2302 361 375 1302 122 120 495 23Mole vapor-fra 0.925 0 0 0 1 0 0 0H2[wt.-%] 0.01 0 0 0 0.27 0 0 0CO [wt.-%] 0.11 0 0 0 2.13 0 0 0CO2[wt.-%] 0.53 0 0.01 0.01 9.87 0,09 0.03 0.03H2O [wt.-%] 1.21 0 0.07 0.07 3.92 0.03 0.06 97.26CH4[wt.-%] 0.42 0 0 0 7.97 00.01 0 0C2-C5 [wt.-% 5.12 0.03 0.74 0.74 71.3 15.59 4.33 0.01C6-C10 [wt.- 33.74 3.01 39.75 39.75 4.36 78.45 49.1 0.01C11-C20 [wt- 47.16 50.23 53.55 53.55 0.01 5.32 41.89 0C21 + [wt-%] 8.56 45.07 2.05 2.05 0 0 1.56 0HA [wt.-%] 3.12 1.66 3.84 3.84 0.16 0.5 3.03 2.7D86-0 % [°C] 172 79 79 - -20 14D86-50 % [°C 335 205 205 - 126 172D86-100 % [° 540 345 345 - 201 340Stream S9 has a final boiling point of 340 °C and, accordingly, is suited as a feedstock for a steam cracking process. Said desired final boiling point FPB of stream S9 was reached by separating 36.1 wt.-% of stream S2 (calculated from total mass flow S2 = 1000 kg / h (Table 1) and total mass flow S5 = 361 kg / h (Table 4)) in step (iv) as high boiling fraction S5 from the gaseous pyrolysis effluent S2. Said process is less energy consuming than processes known from prior art because no additional process step such as distillation is required to produce a pyrolysis oil fraction which is suited as feedstock for a steam cracking process. Example 4The target product is a stream S9 having a final boiling point FBP (determined according to ASTM-D86-23) of 196 °C. Such a stream S9 is suited as a feedstock for producing C2-C4 olefins and C6-C8 aromatic hydrocarbons by steam cracking, particularly a steam cracking unit optimized for naphtha-type feedstocks. The respective mass fractions are given in wt.-%.Table 5: results from example 4.S4 S5 S6a S6b S7 S8 S9 S10T [°C] 189.7 189.7 - 97 25 25 25 25P [bar (abs.)]1.2 1.2 - 1.2 1.1 1.1 3 3Total mass flow [kg / h] 3003 678 0 2003 163 159 159 1Mole vapor-frac 0.868 0 0 0 1 0 0 0H2[wt.-%] 0.01 0 - 0 0.2 0 0 0CO [wt.-%] 0.09 0 - 0 1.6 0 0 0CO2[wt.-%] 0.41 0 - 0.01 7.44 0.03 0.03 0.01H2O [wt.-%] 0.94 0.01 - 0.07 16.24 0.03 0.34 95.19CH4[wt-%] 0.33 0 - 0 5.98 0 0 0C2-C5 [wt-%] 4.2 0.05 - 0.89 59.67 6,88 6.86 0C6-C10 [wt.-%] 55.32 15.43 - 70 8.62 88.44 88.15 0.01C11-C20 [wt-%] 30.92 56.43 - 26.96 0.04 3.77 3.76 0C21+ [wt-%] 5.78 25.12 - 0.16 0 0 0 0HA [wt-%] 2 2.96 - 1.91 0.21 0.84 0.86 4.79D86-0 % [°C] 143 - 71 - 3 3D86-50 % [°C] 275 - 153 - 132 132D86-100 % [°C] 510 - 279 - 196 196Stream S9 has a final boiling point of 196 °C and, accordingly, is suited as a feedstock for a steam cracking process. Said desired final boiling point FPB of stream S9 was reached by separating 67.8 wt-% of stream S2 (calculated from total mass flow S2 = 1000 kg / h (Table 1) and total mass flow S5 = 678 kg / h (Table 5)) in step (iv) as high boiling fraction S5 from the gaseous pyrolysis effluent S2. Said process is less energy consuming than processes known from prior art because no additional process step such as distillation is required to produce a pyrolysis oil fraction which is suited as feedstock for a steam cracking process.Comparative Example 1The process applied in comparative example 1 is shown in Figure 2. The medium boiling fraction is denoted S6' in this comparative example. The gaseous pyrolysis effluent S2 was directly cooled down in a first condensation unit CU1 instead of in a quench unit QU and physical contact with stream S6b (examples 1 to 4). No high boiling stream S5 is separated from the gaseous pyrolysis effluent S2. This results in a final boiling point FBP (D86-100 %) of 490 °C which renders said stream S9 not suitable as a feedstock for steam cracking. Further energy consuming process steps such as distillation are required to obtain a feedstock for steam cracking. The respective mass fractions are given in wt-%.Table 6: results from comparative example 1 .S6' S7 S8 S9 S10T [°C] 97 25 25 25 25 p [bar (abs.)] 1.2 1.1 1.1 3 3Total mass flow [kg / h] 761 120 96 857 23Mole vapor-frac 0 1 0 0 0H2[wt.-%] 0 0.27 0 0 0CO [wt.-%] 0 2.16 0 0 0CO2[wt-%] 0 10.03 0.11 0.02 0.03H2O [wt-%] 0.06 3.05 0.03 0.06 97.58CH4[wt-%] 0 8.1 0.02 0 0C2-C5 [wt-%] 0.55 72.23 18.39 2.54 0.01C6-C10 [wt.-%] 23.87 3.99 76.08 29.7 0.01C11-C20 [wt-%] 50.43 0.01 4.92 45.35 0C21 + [wt-%] 22.38 0 0.01 19.88 0HA [wt-%] 2.71 0.15 0.46 2.46 2.38D86-0 % [°C] 86 - -22 19D86-50 % [°C] 251 - 123 235D86-100 % [°C] 503 - 203 490No high boiling fraction S5 was separated from the gaseous pyrolysis effluent S2 after the quenching of said gaseous pyrolysis effluent S2. The resulting pyrolysis oil stream S9 has a final boiling point FBP of 490 °C and is not suited as a feedstock for a steam cracking process. Further reduction of the final boiling point FBP is an energy consuming process such as distillation is necessary to obtain a fraction of said pyrolysis oil stream suited as feedstock for a steam cracking process.Comparative Example 2The process applied in comparative example 2 is shown in Figure 3 and based on the teachings ofCN 1094567887 A and WO 2023200961 A1 which both include a quench unit but not separating a liquid and a gaseous phase comprised in said first intermediate stream S4 (wherein said liquid phase comprises or consists of said high boiling fraction S5 and wherein said gaseous phase comprises or consists of a second gaseous intermediate stream S4').Accordingly, the gaseous pyrolysis effluent S2 is quenched in the quench unit QU. As opposed to the present invention no high boiling stream S5 is separated from the gaseous pyrolysis effluent S2. The mixing ratio of hot oil gas and cold cracking oil in the quench cooler is 1 :1 , and the temperature after quenching is 275.9 °C. The final condensation temperature of the oil-gas condenser is 25 °C. The respective mass fractions are given in wt-%.Table 7: results from comparative example 2.S4 S5 S6a S6b S7 S8 S9 S10T [°C] 275.9 0 97 97 25 25 25 25 p [bar (abs.)] 1.2 0 1.2 1.2 1.1 1.1 3 3Total mass flow [kg / h] 2000 0 761 1000 120 96 857 23Molar vapor-frac 0.926 0 0 0 1 0 0 0H2[wt.-%] 0.02 0 0 0 0.27 0 0 0CO [wt.-%] 0.13 0 0 0 2.16 0 0 0CO2[wt.-%] 0.61 0 0 0 10.03 0.11 0.02 0.03H2O [wt.-%] 1.38 0 0.06 0.06 3.05 0.03 0.06 97.58CH4[wt-%] 0.49 0 0 8.10 0.02 0 0C2-C5 [wt-%] 5.69 0 0.55 0.55 72.23 18.39 2.54 0.01C6-C10 [wt.-%] 24.89 0 23.87 23.87 3.99 76.08 29.70 0.01C11-C20 [wt-%] 44.64 0 50.43 50.43 0.01 4.92 45.35 0C21+ [wt-%] 19.70 0 22.38 22.38 0 0.01 19.88 0HA [wt-%] 2.44 0 2.71 2.71 0.15 0.46 2.46 2.38D86-0 % [°C] 86 86 - -22 19D86-50 % [°C] 251 251 - 123 235D86-100 % [°C] 503 503 - 203 490No high boiling fraction S5 was separated from the gaseous pyrolysis effluent S2. The resulting pyrolysis oil streamS9 has a final boiling point FBP of 490 °C and is not suited as a feedstock for a steam cracking process. Further reduction of the final boiling point FBP is an energy consuming process such as distillation is necessary to obtain a fraction of said pyrolysis oil stream suited as feedstock for a steam cracking process.

Claims

Claims1 . Process for separating a high boiling fraction from a plastic waste pyrolysis effluent, said process comprising the steps(i) providing a feed stream S1 , wherein said feed stream S1 comprises or preferably consists of plastic waste,(ii) converting said feed stream S1 by pyrolysis in at least one pyrolysis unit PU into a solid residue S3 and a gaseous pyrolysis effluent S2, wherein said gaseous pyrolysis effluent S2 comprises a high boiling fraction S5, a medium boiling fraction S6, a low boiling fraction S8, a non-condensable stream S7 and optionally water,(iii) quenching said gaseous pyrolysis effluent S2 in at least one quench unit QU with a quench medium QM and thereby forming a first intermediate stream S4, wherein said gaseous pyrolysis effluent S2 and said quench medium QM are physically contacted in the at least one quench unit QU and wherein said first intermediate stream S4 comprises a liquid and a gaseous phase, wherein said quench medium QM is selected from the group comprising or preferably consisting of second medium boiling fraction S6b optionally separated in step (vii), medium boiling fraction S6 condensed and separated in step (v), mixtures thereof, and mixtures thereof further comprising at least one further oil FO, wherein said first intermediate stream S4 has a temperature of 180 to 350 °C when leaving the at least one quench unit QU,(iv) separating said liquid and a gaseous phase comprised in said first intermediate stream S4, wherein said liquid phase comprises or consists of said high boiling fraction S5, and wherein said gaseous phase comprises or consists of a second gaseous intermediate stream S4',(v) condensing and separating a fraction of said second gaseous intermediate stream S4' in a first condensation unit CU1, wherein said condensed and separated fraction comprises or consists of said medium boiling fraction S6, and wherein the remaining gaseous fraction of said second gaseous intermediate stream S4' comprises or consists of a third gaseous intermediate stream S4",(vi) condensing and separating a fraction of said third intermediate stream S4" in a second condensation unit CU2, wherein said condensed and separated fraction comprises or consists of said low boiling fraction S8 and optionally water, and wherein and the remaining gaseous fraction of said third gaseous intermediate stream S4" comprises or consists of said non-condensable stream S7,(vii) optionally dividing said medium boiling fraction S6 in a splitting unit SPU into at least two portions, wherein the first portion is a first medium boiling fraction S6a, wherein the second portion is a second medium boiling fraction S6b, and wherein said second medium boiling fraction S6b is physically contacted in step (iii) as quench medium QM with the gaseous pyrolysis effluent S2 in the at least one quench unit QU, and(viii) optionally combining the first medium boiling fraction S6a and the low boiling fraction S8 in a mixing unit MU to obtain a stream S9.

2. Process according to claim 1 wherein 20 to 70 wt.-%, preferably 20 to 40 wt.-% of stream S2 are separated in step (iv) as high boiling fraction S5 therefrom.

3. Process according to claim 1 or 2 wherein said gaseous pyrolysis effluent S2 has a temperature of preferably 250 to 900 °C, more preferably 300 to 700 °C and most preferably 350 to 550 °C when entering the at least one quench unit QU.

4. Process according to any one of claims 1 to 3 wherein the at least one quench unit QU is selected from the group comprising or preferably consisting of tangential-injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of the quench medium QM, and counter-flow washers.

5. Process according to any one of claims 1 to 4 wherein the separation unit SU is selected from the group comprising or preferably consisting of gravity separators, centrifugal separators, filter vane separators, liquid / gas coalescers, and combinations thereof.

6. Process according to any one of claims 1 to 5 wherein the high boiling fraction S5 comprises C11 -C21 + hydrocarbons.

7. Process according to any one of claims 1 to 6 wherein at least a portion of the high boiling fraction S5 is subjected as a feedstock or co-feedstock to a process selected from the group comprising or preferably consisting of partial oxidation, fluid catalytic cracking, hydrocracking, coking, visbreaking and other refining processes.

8. Process according to any one of claims 1 to 7 wherein said medium boiling fraction S6 comprises C6-C20 hydrocarbons.

9. Process according to any one of claims 1 to 8 wherein the weight ratio “S6a : S6b” preferably ranges from 0 to 1, more preferably 0.1 to 0.8 and most preferably 0.2 to 0.6.

10. Process according to any one of claims 1 to 9 wherein the temperature of said quench medium QM when physically contacted with said gaseous pyrolysis effluent S2 in the at least one quench unit QU preferably ranges from 10 to 200 °C, more preferably 50 to 150 °C and most preferably 80 to 120 °C.

11. Process according to any one of claims 1 to 10 wherein said low boiling fraction S8 comprises C6-C10 hydrocarbons.

12. Process according to any one of claims 1 to 11 wherein the quench medium QM consists of one member selected from the group consisting of the liquid second medium boiling fraction S6b, the liquid medium boiling fraction S6, mixtures thereof, and mixtures thereof further comprising at least one further oil FO.

13. Process according to any one of claims 1 to 12, comprising steps (i) to (viii) and further comprising step (ix): feeding at least a portion of stream S9 into a steam cracking unit.

14. Process according to any one of claims 1 to 13, further comprising the step: converting at least one of the streams S5, S6a, S8, and / or optional stream S9 into a product PRF1.

15. Process according to claim 14 wherein the product PRF1 is selected from: i) building block or monomer; or ii) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; orHi) industrial use polymer, industrial use surfactant, descaling compound, industrial use biocide, industrial use solvent, industrial use dispersant, composition thereof or formulation thereof; or iv) agrochemical composition, agrochemical formulation auxiliary or agrochemically active ingredient; or v) active pharmaceutical ingredient or intermediate thereof, pharmaceutical excipient, animal feed additive, human food additive, dietary supplements, aroma chemical or aroma composition; or vi) aqueous polymer dispersion, preferably polyurethane or polyurethane - poly(meth)acrylate hybrid polymer dispersion, emulsion, binder for paper and fiber coatings, UV-curable acrylic polymer for hot melts and coatings polyisocyanates, hyperbranched polyester polyol, polymeric dispersant for inorganic binder compositions, unsaturated polyester polyol or 100% curable composition; or vii) cosmetic surfactant, emollient, wax, cosmetic polymer, UV filter, further cosmetic ingredient or composition or formulation thereof; or viii) polymer B, polymer composition B, coating composition, other functional composition, foil, molded body, coating or coated substrate.

16. Pyrolysis plant for separating a high boiling fraction from a plastic waste pyrolysis effluent comprising a) at least one pyrolysis unit PU, b) at least one quench unit QU, wherein said at least one quench unit QU is downstream of and fluidically connected to said at least one pyrolysis unit PU, c) at least one separation unit SU, wherein said at least one separation unit SU is downstream of and fluidically connected to said at least one quench unit QU, wherein the quench medium comprises or preferably consists of the medium boiling fraction S6b, d) at least one first condensation unit CU1, wherein said at least one first condensation unit CU1 is downstream of and fluidically connected to said at least one separation unit SU,e) at least one second condensation unit CU2, wherein said at least one second condensation unit CU2 is downstream of and fluidically connected to said at least one first condensation unit CU1, f) optionally at least one splitting unit SPU, wherein said at least one splitting unit SPU is downstream of and fluidically connected to said at least one first condensation unit CU1, and g) optionally at least one mixing unit MU, wherein said at least one mixing unit is downstream of and fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2.

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