Process for treating pyrolysis oils in a steam cracking unit

Abstract

The present invention relates to a process for treating at least one pyrolysis oil PO in a steam cracking unit whereby said at least one pyrolysis oil PO is used as a quench medium in a second quench unit in the downstream section of said steam cracking unit. Thereby, the at least one pyrolysis oil PO is separated into a stream PO1 and a stream PO2, whereby said first cooled effluent CE1 is separated into a stream CE1a and a stream CE1b, whereby said stream PO1 and said stream CE1a form a stream POCE1 in said second quench unit QU2, which stream POCE1 leaves said second quench unit QU2. Said stream PO2 and said stream CE1b form a stream POCE2 in said second quench unit QU2, which stream POCE2 leaves said second quench unit QU2. C2-C4 alkenes and / or C6-C8 aromatic hydrocarbons separated from stream POCE1 and / or stream POCE2, respectively, can optionally be converted into a product PRF1.

Description

Process for treating pyrolysis oils in a steam cracking unitTechnical areaThe present invention relates to pyrolysis oils manufactured from pyrolysis of plastic waste as feedstock for steam cracking processes.Background of the inventionPyrolysis oils made by pyrolysis from plastic waste are used for different applications, for example as fuels for heat generation, as feedstock for production of synthesis gas and feedstock for cracking processes such as steam cracking and fluid catalytic cracking. The requirements for such applications differ. For example, the boiling range of such pyrolysis oils does not fulfil the requirements for feedstocks used in a steam cracking process because such pyrolysis oils comprise high-boiling components which must be separated from the desired low-boiling portion suited as feedstock for steam cracking processes. Said portions can be for example separated by distillation which is an energy consuming process because the pyrolysis oil needs to be heated to a temperature sufficient to evaporate and thereby separate the desired low-boiling portion from the high-boiling portion. Furthermore, components such as dienes typically comprised in pyrolysis oils cause undesired fouling in distillation columns or need to be separated by expensive processes such as hydrotreatment before subjecting the pyrolysis oil to a distillation.In addition, precious components such as (light) alkenes and C6-C8 aromatic hydrocarbons comprised in pyrolysis oils are cracked and thereby lost in case the light-boiling portion of a pyrolysis oil is used as a feedstock for a cracking process.Document WO 2024 / 030747 A1 refers to processes and facilities for producing a recycled content organic compound directly or indirectly from waste plastic. Recycle-content para-xylene ("r-paraxylene”) converted into recycle-content terephthalic acid and / or recycle-content polyethylene terephthalate. Waste plastic is converted into a plastic waste pyrolysis oil which is then subjected to a steam cracking process. The steam cracking process results in light olefins and "r-pyrolysis gasoline” like the steam cracking of fossil feedstocks such as naphtha derived from fossil oil which results in light olefins and pyrolysis gasoline. The "r-pyrolysis gasoline” is a standard steam cracking side product which comprises a mixture of aromatic compounds. Said "r-pyrolysis gasoline” is then fed into an "aromatic complex” in which aromatic compounds such as "r-paraxylene” are separated. Accordingly, the desired aromatic compounds present in the pyrolysis oil are subjected to a steam cracking process whereby at least a portion of said desired aromatic components is cracked into non-aromatic compounds.Document WO 2023 / 178146 A1 refers to a process in which (Figure 1) mixed plastic waste is converted into a "r- pyoil” and a "r-pygas”. Said "r-pyoil” is then fed into a cracking process such as a steam cracking process and said "r- pygas” is fed into stream between a quench unit and a compression unit and / or into a stream between a compression unit and a separation unit.It is an objective of the present invention to provide to increase the yield of C6-C8 aromatics separation from pyrolysis oils formed in the pyrolysis of plastic waste.It is a further objective of the present invention to provide to increase the yield of C2-C4 alkene separated from pyrolysis oils formed in the pyrolysis of plastic waste.Summary of the inventionThese objectives are solved by a process for treating a pyrolysis oil in a steam cracking unit, wherein said steam cracking unit comprises a) at least one steam cracking oven SCO, b) a first cooling unit CU1 wherein said first cooling unit CU1 is downstream of and fluidically connected to said at least one cracking oven SCO, c) a first quench unit QU 1, wherein said first quench unit QU1 is downstream of and fluidically connected to said first cooling unit CU1, d) and a second quench unit QU2 wherein said second quench unit QU2 is downstream and fluidically connected to said first quench unit QU1, said process comprising the steps(i) providing a first feedstock F1, a water stream W, a quench oil QO and at least one pyrolysis oil PC, wherein the at least one pyrolysis oil PC is manufactured by pyrolysis from plastic waste and wherein said at least one pyrolysis oil PC comprises 02-04 alkenes and 06-08 aromatic hydrocarbons,(ii) feeding said first feedstock F1 into said at least one steam cracking oven SCO and thereby forming an effluent E which leaves said at least one steam cracking oven SCO,(iii) feeding said effluent E into said first cooling unit CU1 whereby heat is transferred from said effluent E to said water stream W and thereby a cooled effluent CE is formed from said effluent E and wherein said effluent and said water stream W are indirectly contacted in said first cooling unit CU1 with each other,(iv) feeding said cooled effluent CE into said first quench unit QU1 and directly contacting said cooled effluent CE with said quench oil QO in said first quench unit QU1 and thereby separating said cooled effluent CE into a first cooled effluent CE1 and a second cooled effluent CE2 which both leave said first quench unit QU1 wherein the second cooled effluent CE2 comprises said quench oil QO after said quench oil QO was directly contacted with said cooled effluent CE, and(v) contacting said at least one pyrolysis oil PC with said first cooled effluent CE1 inside said second quench unit QU2, whereby said at least one pyrolysis oil PC is separated into a stream P01 and a stream P02, whereby said first cooled effluent CE1 is separated into a stream CE1a and a stream CE1 b, whereby said stream P01 and said stream CE1a form a stream P0CE1 in said second quench unit QU2, which stream P0CE1 leaves said second quench unit QU2 and whereby said stream P02 and said stream CE1b form a stream P0CE2 insaid second quench unit QU2, which stream P0CE2 leaves said second quench unit QU2, said stream P0CE2 comprising C6-C8 aromatic hydrocarbons.C2-C4 alkenes and C6-C8 aromatic hydrocarbons comprised in the at least one pyrolysis oil PO can be separated therefrom by an energy efficient method using the second quench unit QU2 which is comprised in existing steam cracking units by using said at least one pyrolysis oil PO which is directly contacted with the cooled effluent CE1. The temperature of said cooled effluent CE1 is high enough to separate the C6-C8 aromatic hydrocarbons of the pyrolysis oil comprised in stream POCE2 from C2-C4 alkenes comprised in stream POCE1. C2-C4 alkenes and C6-C8 aromatic hydrocarbons can be separated in successive process steps from stream POCE1 and POCE2, respectively. POCEIa, the remaining portion of stream POCE1, and / or POCE2a, the remaining portion of stream POCE2, can then be used as a cracker feedstock (and optionally methane and / or hydrogen comprised in POCEIa, and separated therefrom further downstream, as a fuel for providing heat to the at least one steam cracking oven SCO). In addition, the cooled effluent CE1 is further cooled inside the second quench unit QU2 by direct contacting said cooled effluent CE1 with the at least one pyrolysis oil PO. Accordingly, the at least one pyrolysis oil PO has the function of a quench medium in said second quench unit QU2. Furthermore, undesired coking inside the at least one steam cracking oven SCO is reduced when using stream POCEIa and / or POCE2a which are depleted in C2-C4 alkenes and / or C6-C8 aromatic hydrocarbons, instead of the at least one pyrolysis oil PO not subjected to the process according to the present invention as a feedstock for said at least one steam cracking oven SCO which would still comprise 02-04 alkenes and 06-08 aromatic hydrocarbons which cause undesired coking inside the at least one steam cracking oven SCO.The 06-08 aromatics comprised in a pyrolysis oil PO are directly separated therefrom in a secondary quench unit QU2 by contacting said pyrolysis oil PO with a stream of water W and a stream CE1 . Thereby, the yield in 06-08 aromatics separated directly from said pyrolysis oil PO is increased because the degradation of at least a portion of said 06-08 aromatics comprised in the pyrolysis oil PO, when subjected to a steam cracking process, is avoided. In case stream(s) POCEIa and / or P0CE2 is / are utilized as a feedstock for successive steam cracking, the overall yield of C6-C8 aromatics derived from said pyrolysis oil PO is even more increased.Furthermore, 02-04 alkenes comprised in the at least one pyrolysis oil are also separated (enriched in fraction P01). In case stream POCEIa is then utilized as a feedstock for successive steam cracking (Figure 5), the overall yield in C2-C4 alkenes obtained from the at least one pyrolysis oil is increased.Figure 1 shows the process according to the first embodiment of the present invention.Figure 2 shows the first quench unit QU1 and the second quench unit QU2 of the process according to the present invention in more detail.Figure 3 shows the aromatic extraction unit AEU downstream of the second quench unit QU2.Figure 4 shows the aromatic extraction unit AEU and the separation unit SU, both downstream of the second quench unit QU2.Figure 5 shows the utilization of streams POCEIa and POCE2b as co-feedstocks for the at least one steam cracking oven SCO.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.The term “downstream of” is defined herein in respect to a succession of unit operations as located next to 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 through and / 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 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 as interrupted by e.g., an additional unit, storage tank(s), transporting a stream by for example by truck or train or in a pipeline.“Pyrolysis gasoline” (CAS Number: 68477-58-7) is a side product of a steam cracking process with a high aromatics content. Pyrolysis gasoline can be for example separated from a steam cracked pyrolysis oil as described in WO2024 / 030747 A1 and WO 2023 / 178146 A1. Accordingly, pyrolysis gasoline and pyrolysis oils manufactured by pyrolysis from plastic waste are different hydrocarbon-containing mixtures.The process for treating pyrolysis oils in a steam cracking unit according to the present invention is described in detail below (Figure 1 and Figure 2).A first feedstock F1 is provided which then enters at least one steam cracking oven SCO, preferably a fired tubular reactor, more preferably a fired radiant tube or a fired radiant coil reactor in which, under a controlled residence time of about 0.1 to about 0.5 s, a temperature profile by which the (pre-heated) first feedstock F1 is heated from a temperature of 500 to 650 °C to a temperature of 750 to 900 °C. During this short reaction time hydrocarbons in the feedstock F1 are cracked into smaller molecules such as 02-04 alkenes and 06-08 aromatic hydrocarbons. The first feedstock F1 is preferably pre-heated to a temperature of 500 to 650 °C in a convection zone upstream of the at least one steam cracking oven SCO. Said convection zone preferably comprises at least one heat exchanger in which the first feedstock F1 is preheated to the desired temperature before inserted into the at least one steam cracking oven SCO.A steam cracking unit preferably comprises more than one steam cracking oven SCO which are most preferably operated as an array of parallel steam cracking ovens SCO.The first feedstock F1 is converted in the at least one steam cracking oven SCO into an effluent E which leaves the at least one steam cracking oven at a temperature of about 750 to about 900 °C.Optionally, at least a portion of the stream POCE1 a and / or at least a portion of the stream POCE2a are combined with the first feedstock F1, preferably before entering the at least one steam cracking oven SCO, more preferably before entering the convection zone upstream of the at least one steam cracking oven SCO. The streams POCEIa and POCE2a are described in detail further below.Steam cracking ovens SCO 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”, subchapter "5.1.4 Commercial Cracking Ovens”, pages 482 to 490, 2012 Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim (DOI: 10.1002 / 14356007.a10_045.pub3).Examples of steam cracking units comprising at least one steam cracking oven which are suited for the process according to the present invention comprise ABB Lummus Global Furnace, Millisecond Furnace (KBR, Houston Texas), Shaw Furnace (The Shaw Group, Baton Rouge, USA), Technip Furnace (Technip, Paris, France), Linde-Pyrocrack Furnace (Linde AG, Munich, Germany, terraced-wall furnace (Foster & Wheeler Energy Corp., Livingston, N.J.), and Mitsui advanced cracker (Mitsui Engineering & Shipbuilding Co., Tokyo, Japan).In one aspect of the present invention, the at least one steam cracking oven SCO is at least partially heated with electrical energy, preferably electrically energy provided by a renewable source such as solar energy, wind energy and tidal energy.Next, the effluent E leaving the at least one steam cracking oven SCO a temperature of about 750 to about 900 °C is cooled to a temperature of 300 to 600 °C, more preferably 350 to 500 °C and most preferably 380 to 450 °C, preferably within 0.02 to 0.1 s in a first cooing unit CU1. Such rapid cooling is preferred to prevent degradation of the highly reactive products such as dienes comprised in effluent E by secondary reactions and thereby causing undesired fouling and / or coking and yield reduction of desired products (preferably 02-04 alkenes and 06-08 aromatic hydrocarbons).The effluent E is cooled in the first cooling unit CU1 by indirect heat exchange with a stream of water W as heat transfer medium whereby the water is evaporated, and steam is formed therefrom. The steam then leaves the first cooling unit CU1 as stream W1. Accordingly, the effluent E and the heat transfer medium are not in physical contact with each other inside the first cooling unit CU1 and the heat is transferred from the effluent E to a solid material (e.g., the wall of a pipe made of metal or a metal alloy) and from there to the heat transfer medium.The first cooling unit CU1 is also known as "transfer-line exchanger” (TLE). Preferably, cooling of effluent E in the first cooling unit CU1 is achieved by vaporization of a high-pressure boiler feed water (“BFW”), preferably having a pressure of 6 to12 MPa), which BFW is preferably superheated in the convection section to high-pressure superheated steam ("HPSS”) having a pressure of 6 to 12 MPa. Thereby, effluent E is cooled down to a temperature of 300 to 600 °C, more preferably 350 to 500 °C and most preferably 380 to 450 °C. The effluent E is cooled in the first cooling unit CU1 and then leaves the first cooling unit CU1 as a cooled effluent CE.The first cooling unit CU1 is preferably a heat exchanger such as shell-and-tube exchanger, tunnel-flow exchanger, double-pipe exchanger, double-pipe-linear exchanger, multi-double-pipe exchanger, double-pipe-linear exchanger. Such heat exchangers can be mounted horizontally or vertically.The cooled effluent CE is further cooled by direct heat exchange in a first quench unit QU1 by contacting said cooled effluent CE inside said first quench unit QU1 with a quench oil QO. Accordingly, the cooled effluent CE and the quench oil QO are in physical contact with each other inside the first quench unit QU1 . Thereby, said cooled effluent CE is separated into a stream CE1 and a stream CE2. The stream CE2 leaves the first quench unit QU1 mixed together with the quench oil QO.Said cooled effluent CE preferably has a temperature of 300 to 600 °C, more preferably 350 to 500 °C and most preferably 380 to 450 °C when entering the first quench unit QU1 .Said quench oil QO preferably has a temperature below 80 to 140 °C, more preferably below 100 to 130 °C and most preferably below 105 to 125 °C when entering the first quench unit QU1.The quench oil QO is preferably selected from the group comprising or preferably consisting of hydrocarbons or a mixture of hydrocarbons having a boiling point BP which is higher than the temperature T of the stream POE2. Such quench oils QO are known in the art and the skilled person can choose a quench oil QO for a given application accordingly.Said first quench unit QU1 comprises at least a first inlet 11 and a second inlet I2 and at least a first outlet 01 and a second outlet 02. Preferably, said quench oil QO is fed into said first quench unit QU1 through said first inlet 11. Preferably, said cooled effluent CE is fed into said first quench unit QU1 through said second inlet I2. Preferably, said stream CE2 leaves said first quench unit QU1 through said first outlet 02 mixed with the quench oil QO. Preferably, said stream CE1 leaves said first quench unit QU1 through said second outlet 01.Stream CE2 comprises 09+ hydrocarbons, such as n-decane, n-undecane, n-dodecane and stereoisomers thereof, and is depleted in 06-08 aromatic hydrocarbons, 02-04 alkenes and 01 -08 alkanes (including straight chain, branched and cyclic isomers), preferably 06-08 aromatic hydrocarbons, 02-04 alkenes and 01 -04 alkanes.Stream CE1 comprises 06-08 aromatic hydrocarbons, 02-04 alkenes and 01 -08 alkanes (including straight chain, branched and cyclic isomers), preferably 06-08 aromatic hydrocarbons, 02-04 alkenes and 01 -04 alkanes, and is depleted in 09+ hydrocarbons, such as n-decane, n-undecane, n-dodecane and stereoisomers thereof.Said first quench unit QU1 is preferably selected from the group comprising tangential-injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of said at least one pyrolysis oil PO, counter-flow washers and the like. The skilled person can choose a suitable type of available quench methods and units as first quench unit QU1.Said stream CE1 is fed into a second quench unit QU2 which is downstream of the first quench unit QU1 and which is fluidically connected to said outlet 01 of said first quench unit QU1 . The stream CE1 has a temperature before entering the second quench unit QU2 of preferably 80 to 140 °C, more preferably 100 to 130 °C and most preferably 105 to 125 °C. The stream CE1 preferably enters said second quench unit QU2 through inlet I4. The stream CE1 is separated in the second quench unit QU2 into a stream CE1 a and a stream CE1 b. Said stream CE1a is enriched in C2-C4 alkenes and enriched in C1-C4 alkanes compared to stream CE1. Said stream CE1 a is depleted in C6-C8 aromatic hydrocarbons compared to stream CE1. Said stream CE1 b is depleted in C2-C4 alkenes and depleted in C1-C4 alkanes compared to stream CE1. Said stream CE1 a is enriched in C6-C8 aromatic hydrocarbons compared to stream CE1.At least one pyrolysis oil PO is fed into the second quench unit QU2, preferably through the inlet I3 (Figure 2). The at least one pyrolysis oil PO is manufactured by pyrolysis of plastic waste. This is described in detail further below. The at least one pyrolysis oil PO comprises 02-04 alkenes and 06-08 aromatic hydrocarbons. The at least one pyrolysis oil PO is separated in the second quench unit QU2 into a stream P01 and a stream P02. Said stream P01 is enriched in 02-04 alkenes and enriched in 01-04 alkanes compared to the at least one pyrolysis oil PO. Said stream P01 is depleted in 06-08 aromatic hydrocarbons compared to the at least one pyrolysis oil PO. Said stream P02 is depleted in 02-04 alkenes and depleted in 01-04 alkanes compared to said at least one pyrolysis oil PO. Said stream P02 is enriched in 06-08 aromatic hydrocarbons compared to said at least one pyrolysis oil PO.The at least one pyrolysis oil PO is used to separate 06-08 aromatic hydrocarbons comprised in the cooled cracker effluent CE from 02-04 alkenes and 01-04 alkanes also comprised in the cooled cracker effluent CE. Thereby, also 06-08 aromatic hydrocarbons comprised in the at least one pyrolysis oil PO are separated from 02-04 alkenes and 01-04 alkanes also comprised in the at least one pyrolysis oil PO, wherein said at least one pyrolysis oil PO is manufactured (obtained by) pyrolysis of plastic waste. Preferably, the effluent E from which the cooled cracker effluent CE is formed is manufactured (obtained by) steam cracking.Said stream CE1 is quenched in said second quench unit QU2 with a stream of at least one pyrolysis oil PO and thereby separated into streams CE1a and CE1b as described above. The stream of said at least one pyrolysis oil PO has a temperature before entering the second quench unit QU2 of preferably 40 to 75 °C, more preferably 50 to 70 °C and most preferably 55 to 65 °C. Preferably, the stream of said at least one pyrolysis oil PO is entering the second quench unit QU2 at atmospheric pressure.Said stream CE1a leaves said second quench unit QU2 mixed with said stream P01 as stream P0CE1, preferably through outlet 03. Said stream CE1b leaves said second quench unit QU2 mixed with said stream P02 as stream P0CE2, preferably through outlet 04.The stream P0CE1 preferably has a temperature of 20 to 50 °C, more preferably 25 to 45 °C and most preferably 30 to 40 °C when leaving the second quench unit QU2. Thereby, said stream POCE1 is enriched in 02-04 alkenes and enriched in 01-04 alkanes. Thereby, said stream POCE1 is depleted in 06-08 aromatic hydrocarbons, because said 06-08 aromatic hydrocarbons already condense at much higher temperatures (boiling points: benzene (80.1 °C), toluene (110.6 °C), xylene isomers (138 to 144 °C) and ethylbenzene (136 °C)).The stream POCE2 preferably has a temperature of 65 to 100 °C, more preferably 70 to 95 °C and most preferably 75 to 90 °C when leaving the second quench unit QU2. Thereby, said stream POCE2 is enriched in 06-08 aromatic hydrocarbons. Thereby, said stream POEC2 is depleted in 02-04 alkenes and depleted in 01-04 alkanes. Thereby, said stream POEC2 is enriched in 06-08 aromatic hydrocarbons.Said second quench unit QU2 is preferably selected from the group comprising tangential-injection mixing devices, static mixers, vessels comprising at least one spray-nozzle for insertion of said at least one pyrolysis oil PO, counterflow washers and the like. The skilled person can choose a suitable type of available quench methods and units as second quench unit QU2.Preferably, said stream POCE2 comprising sub-stream PO2 is fed into an optional aromatics extraction unit AEU which is downstream of the second quench unit QU2 of the second quench unit QU2 (Figure 3). An aromatics-rich stream P0CE2b is separated from said stream POCE2 in the aromatics extraction unit AEU, wherein said aromatics- rich stream P0CE2b is enriched in C6-C8 aromatic hydrocarbons and comprises at least one of benzene, toluene and / or xylene isomers and wherein the remaining stream POCE2a is depleted in C6-C8 aromatic hydrocarbons.Preferably, C6-C8 aromatic hydrocarbons comprised in stream P0CE2b are further separated in said aromatic hydrocarbon extraction unit AEU into a stream ASa which is enriched in benzene, a stream ASb which is enriched in toluene, a stream ASc which is enriched in C8 aromatic hydrocarbons (ethylbenzene, 1 ,2-xylene, 1 ,3-xylene, 1,4- xylene) and a stream POCE2a which is depleted in C6-C8 aromatic hydrocarbons.The aromatic hydrocarbon extraction unit AEU is downstream of and fluidically connected to the second quench unit QU2, preferably fluidically connected to the second outlet 04 of the second quench unit QU2.The aromatic hydrocarbon extraction unit AEU can be any unit operation suitable to separate C6-C8 aromatic hydrocarbons comprised in stream P0CE2b into a stream ASa, a stream ASb, a stream ASc and a stream POCE2a. For example, the optional aromatic hydrocarbon extraction unit AEU can comprise at least one selective adsorption unit operation, at least one selective absorption unit operation, at least one extractive distillation unit operation, at least one solvent extraction followed by distillation and combinations thereof. Suitable aromatic hydrocarbon extraction units AEU are commercially available, for example the Morphylane® extractive distillation process by Uhde.The stream ASa preferably comprises at least 90 wt.-% benzene, more preferably at least 95 wt.-% benzene and most preferably at least 99 wt.-% benzene. The stream ASb preferably comprises at least 90 wt.-% toluene, more preferably at least 95 wt.-% toluene and most preferably at least 99 wt.-% toluene. The stream ASc preferably comprises at least 90 wt.-% of xylene isomers and about 10 wt.-% of nonaromatic Cs+ components, more preferably at least 93 wt.-% of xylene isomers and about 2.5 wt.-% nonaromatic Cs+ components.The stream POCE2a is suited as a feedstock for cracking processes such as (fluid) catalytic cracking, thermal cracking and steam cracking, most preferably a steam cracking process (Figure 5). Preferably, the stream POCE2a is combined with the first feedstock F1 and co-fed into the at least one steam cracking oven SCO or fed into a separate steam cracking oven SCO without being combined with the first feedstock F1 . The effluent E and an effluentEPOCE2a which is formed by steam cracking of the stream P0CE2a are then combined in the first cooling unit CU1 in case they were not co-fed into the same steam cracking oven SCO.Optionally, the one or both streams ASb and / or ASc are then fed into a hydroalkylation unit HAU whereby toluene and / or xylene isomers and / or ethylbenzene are converted into benzene. Accordingly, the benzene yield can be increased thereby. Hydroalkylation of alkyl-substituted benzene-derivatives into benzene and corresponding hydroalkylation units HAU are known in the art and are for example described in Ullmann's Encyclopedia of Industrial Chemistry, Vol. 5, Chapter "Benzene” by H. 0. Folkins, pages 246-251, 2012 and in Industrielle organische Chemie, 3rdEd., K. Weissermel, H.-J. Arpe, pages 351-352, 1988 which are both incorporated by reference herein.Preferably, said stream POCE1 is then subjected to, preferably in this order, a process sequence comprising the steps compression, acid-gas removal, drying, hydrocarbon fractionating and hydrotreatment in a separation unit SU and thereby separating C2-C4 alkenes comprised in the stream POCEIb from C1-C4 alkanes comprised in stream POCEIa (Figure 4). Said stream POCEIb is enriched in C2-C4 alkenes and is depleted in C1-C4 alkanes. Said stream POCE2b is depleted in C2-C4 alkenes and enriched in C1-C4 alkanes.Optionally, at least a portion of said remaining stream POCEIa and / or at least a portion of said stream POCE2a is / are fed into at least one steam cracking oven SCO (Figure 5). The at least a portion of stream POCEIa and / or stream POCE2a can be fed in steam cracking ovens SCO separate from those in which the first feedstock is fed or the is mixed with the first feedstock F1 before entering a steam cracking oven SCO. The operation mode is selected by the skilled person based on e.g., impurities present in stream POCEIa and / or stream POCE2a, in this case stream POCEIa and / or stream POCE2a is / are preferably mixed with the first feedstock F1 prior to feeding said streams into a steam cracking oven SCO. Thereby, such impurities are diluted in the combined feedstock fed into the steam cracking oven SCO which is beneficial. In other cases, said feedstocks can be fed in individual steam cracking ovens SCO.The first feedstock F1 is preferably a hydrocarbon or mixture of hydrocarbons also known as "petroleum hydrocarbons”. The first feedstock F1 has a final boiling point FBP (determined according to EN ISO 3405) of no more than 600 °C because higher boiling materials cannot be vaporized under the operating condition of a steam cracking oven SCO. The first feedstock F1 is a liquid or a liquified gas, preferably a liquid or liquified gas selected from the group comprising or preferably consisting of naphtha, pyrolysis oils manufactured by pyrolysis from plastic waste, pyrolysis oils manufactured by pyrolysis from biomass, bio-oils, natural gas liquids, liquified petroleum gas, propane, butane, pentane and mixtures thereof naphtha, gas condensates, preferably the 180 to 350 °C boiling cut thereof which is also known as gas oil, hydrocracker bottoms, preferably the 350 to 600 °C boiling cut thereof, a stream BTX which consists of 30 to 50 wt.-% benzene, 10 to 25 wt.-% toluene, 2 to 8 wt.-% xylene, 4 to 9 wt.-% ethyl benzene and less than 45 wt.-% other components, wherein said other components are selected from cyclopentane, cyclopentene, n- hexane, methyl cyclopentane and methyl cyclopentene, and mixtures thereof.More preferably, the first feedstock F1 is a mixture of hydrocarbons which is liquid at atmospheric pressure. More preferably, the first feedstock F1 is selected from the group comprising naphtha, gas condensates (preferably the 180 to 350 °C boiling cut thereof which is also known as gas oil), hydrocracker bottoms (preferably the 350 to 600 °C boiling cut thereof), a stream BTX which consists of 30 to 50 wt.-% benzene, 10 to 25 wt.-% toluene, 2 to 8 wt.-% xylene, 4 to 9 wt.-% ethyl benzene and less than 45 wt.-% other components, wherein said other components are selected from cyclopentane, cyclopentene, n-hexane, methyl cyclopentane and methyl cyclopentene, and mixtures thereof. In case the first feedstock F1 comprises said stream BTX, fouling inside the steam cracking unit, particularly in the at least one steam cracking oven SCO, can be removed without shutting down the process and no additional components are used for washing. Naphtha can be used as first feedstock F1 in form of "full range” naphtha, light naphtha (preferably the 30 to 90 °C cut of full range naphtha), and heavy naphtha (for example the 90 to 200 °C cut of "full range” naphtha). Naphtha is a hydrocarbon mixture which is liquid at atmospheric pressure and preferably has a boiling point rang of about 30 to about 200 °C. Naphtha can be produced from feedstock such as crude oil, natural gas condensates, petroleum distillates, coal tar and peat by (fractional) distillation. Said naphtha can be substituted at least in part at least partially in the first feedstock F1 by "bio-naphtha” which can be for example produced from biomass by pyrolysis.Said at least one pyrolysis oil PC is manufactured by a pyrolysis reaction from plastic waste.Preferably, said at least one pyrolysis oil PO is manufactured by a pyrolysis reaction from plastic waste wherein said plastic waste is selected from the group comprising polyalkenes, polystyrene, and copolymers thereof, polyvinylchloride (PVC), polyvinylidene chloride (PVDC), polyamides (PA), polyurethanes (PU), acrylonitrile butadiene styrene (ABS), polyesters, polycarbonate (PC), rubbers and mixtures thereof. More preferably, said at least one pyrolysis oil PO is manufactured by a pyrolysis reaction from plastic waste and wherein said plastic waste comprises polyalkenes. Polyalkenes are for example polyethylene (LDPE, HDPE) and polypropylene.Typically, the plastic waste 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. 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 productssuch 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. Pyrolysis oils obtained by pyrolysis of (predominantly) end-of-life tires are also known as tire pyrolysis oils (TPO).Examples of bio waste which can be comprised in "plastic waste” include green waste, food waste, human waste, manure, sewage, sewage sludge and slaughterhouse waste.To obtain the at least one pyrolysis oil PO, the plastic waste is inserted into a pyrolysis reactor using a dosing unit such as a screw or an extruder or a rotary valve or a pneumatic conveyor or a liquid injector. The plastic waste is optionally pre-heated in e.g., a heat exchanger prior to insertion into the pyrolysis reactor and / or subjected to a pre-py- rolysis at a temperature in the range of, for example, from about 200 to about 360 °C. Next, the plastic waste is heated in the pyrolysis reactor to a temperature in the range of from about 350 to about 900 °C, more preferably in the range of from 400 to about 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). The pyrolysis reactor is preferably selected from the group comprising fluidized bed reactors, moving bed reactors, entrained flow reactors, screw reactors, extruders, stirred tank reactors and rotary kiln reactor. Preferably, the pyrolysis is performed in the pyrolysis reactor under an inert atmosphere exempt of oxygen or air.Pyrolysis processes as such are known. They are described, e.g., in EP 0713906 A1 and WO 95 / 03375 A1. Suitable pyrolysis oils PO are also commercially available.Preferably, said at least one pyrolysis oil PO comprises at least one of the following properties: a) 5 to 70 wt.-% < C5 hydrocarbons, preferably 40 to 70 wt.-% < C5 hydrocarbons (determined according to ASTM D D5134) and / or b) 5 to 70 wt.-% C5 to C6 hydrocarbons, preferably 25 to 70 wt.-% C5 to C6 hydrocarbons (determined according to ASTM D 5134) and / or c) 0 to 10 wt.-% C8 to C12 hydrocarbons, preferably 0 to 2 wt.-% C8 to C12 hydrocarbons (determined according to ASTM D 5134) and / or d) 0 to 10 wt.-% > 012 hydrocarbons, preferably 0 to 2 wt.-% > 012 hydrocarbons (determined according to ASTM D 5134) and / or e) 5 to 50 wt.-% 06-08 aromatic hydrocarbons, preferably 5 to 20 wt.-% 06-08 aromatic hydrocarbons (determined according to ASTM D 5134) and / or f) 0 to 2 wt.-% styrene, preferably 0 to 0.5 wt.-% styrene (determined according to ASTM D 5134) and / or g) no more than 500 ppmw sulfur, preferably no more than 250 ppmw sulfur (determined according to ASTM 5453 and / or h) no more than 150 ppmw nitrogen, preferably no more than 50 ppmw nitrogen (determined according to ASTM D 6069) and / ori) no more than 50 ppmw chlorine, preferably no more than 10 ppmw chlorine (determined according to ASTM 5291.More preferably, said at least one pyrolysis oil PO comprises at least two or more of properties a) to I). Most preferably, the at least one pyrolysis oil PO has at least five of properties a) to I).Preferably, said at least one pyrolysis oil PO has j) a final boiling point FBP of 100 to 300 °C, preferably of 150 to 250 °C (determined according to EN ISO 3405) and / or k) a density of 0.6 to 0.8 kg / l, preferably of 0.6 to 0.7 kg / l (determined according to ASTM D 4052).Optionally, said at least one pyrolysis oil PO is subjected to at least one upgrading process before provided in step (I). Said at least one pyrolysis oil PO is preferably subjected to at least one upgrading process before provided in step (I) in case at least one of the properties a) to k) is not within the ranges a) 5 to 70 wt.-% < C5 hydrocarbons, preferably 40 to 70 wt.-% < C5 hydrocarbons (determined according to ASTM D D5134) and / or b) 5 to 70 wt.-% C5 to C6 hydrocarbons, preferably 25 to 70 wt.-% C5 to C6 hydrocarbons (determined according to ASTM D 5134) and / or c) 0 to 10 wt.-% C8 to C12 hydrocarbons, preferably 0 to 2 wt.-% 08 to 012 hydrocarbons (determined according to ASTM D 5134) and / or d) 0 to 10 wt.-% > 012 hydrocarbons, preferably 0 to 2 wt.-% > 012 hydrocarbons (determined according to ASTM D 5134) and / or e) 5 to 50 wt.-% 06-08 aromatic hydrocarbons, preferably 5 to 20 wt.-% 06-08 aromatic hydrocarbons (determined according to ASTM D 5134) and / or f) 0 to 2 wt.-% styrene, preferably 0 to 0.5 wt.-% styrene (determined according to ASTM D 5134) and / or g) no more than 500 ppmw sulfur, preferably no more than 250 ppmw sulfur (determined according to ASTM 5453 and / or h) no more than 150 ppmw nitrogen, preferably no more than 50 ppmw nitrogen (determined according to ASTM D 6069) and / or l) no more than 50 ppmw chlorine, preferably no more than 10 ppmw chlorine (determined according to ASTM 5291. j) a final boiling point FBP of 100 to 300 °C, preferably of 150 to 250 °C (determined according to EN ISO 3405) and / or k) a density of 0.6 to 0.8 kg / l, preferably of 0.6 to 0.7 kg / l (determined according to ASTM D 4052).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. Suchoptional upgrading processes are for example described in WO 2021 / 224287 A1, WO 2023 / 061834 A1, EP 0713906 A1 and WO 95 / 03375 A1 which are incorporated herein by reference. A skilled person knows how and in which cases to use pre-treatment methods disclosed in said documents and comparable pre-treatment methods disclosed elsewhere.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 process for the production of 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 / or steam 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)acrylic acid; in particular sodium, potassium and zinc salts; (meth)acrolein and (meth)acrylates. (Methacrylates 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 andpropylene 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 polymer composition 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”, 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 dispersant”, 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 usesurfactant, 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 agrochemi- cally 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” and "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, Citranax- anthin, 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 andsodium 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 polyvinylimidazole / polyvinylpyrrolidone-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 sesquiterpe- noids, 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 composition 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 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 poly- mer(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 compositions) 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 pol- yol(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 dispersants) 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), asused 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 cosmetic surfactant, 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 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 method 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 method 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, but does not represent the claims of the present invention.1. Process for treating a pyrolysis oil in a steam cracking unit, wherein said steam cracking unit comprises a) at least one steam cracking oven SCO, b) a first cooling unit CU1 wherein said first cooling unit CU1 is downstream of and fluidically connected to said at least one cracking oven SCO, c) a first quench unit QU 1, wherein said first quench unit QU1 is downstream of and fluidically connected to said first cooling unit CU1, d) and a second quench unit QU2 wherein said second quench unit QU2 is downstream and fluidically connected to said first quench unit QU1, said process comprising the steps(I) providing a first feedstock F1, a water stream W, a quench oil QO and at least one pyrolysis oil PC, wherein the at least one pyrolysis oil PC is manufactured by pyrolysis from plastic waste and wherein said at least one pyrolysis oil PC comprises 02-04 alkenes and 06-08 aromatic hydrocarbons,(ii) feeding said first feedstock F1 into said at least one steam cracking oven SCO and thereby forming an effluent E which leaves said at least one steam cracking oven SCO,(ill) feeding said effluent E into said first cooling unit CU1 whereby heat is transferred from said effluent E to said water stream W and thereby a cooled effluent CE is formed from said effluent E and wherein said effluent and said water stream W are indirectly contacted in said first cooling unit CU1 with each other,(iv) feeding said cooled effluent CE into said first quench unit QU1 and directly contacting said cooled effluent CE with said quench oil QO in said first quench unit QU1 and thereby separating said cooled effluent CE into a first cooled effluent CE1 and a second cooled effluent CE2 which both leave said first quench unit QU1 wherein the second cooled effluent CE2 comprises said quench oil QO after said quench oil QO was directly contacted with said cooled effluent CE,(v) contacting said at least one pyrolysis oil PC with said first cooled effluent CE1 inside said second quench unit QU2, whereby said at least one pyrolysis oil PC is separated into a stream P01 and astream PO2, whereby said first cooled effluent CE1 is separated into a stream CE1 a and a stream CE1 b, whereby said stream P01 and said stream CE1 a form a stream POCE1 in said second quench unit QU2, which stream POCE1 leaves said second quench unit QU2 and whereby said stream P02 and said stream CE1 b form a stream POCE2 in said second quench unit QU2, which stream POCE2 leaves said second quench unit QU2, said stream POCE 2 comprising C6-C8 aromatic hydrocarbons.2. Process according to embodiment 1 wherein said at least one pyrolysis oil PO is manufactured by a pyrolysis reaction from plastic waste wherein said plastic waste is selected from the group comprising polyalkenes, polystyrene, and copolymers thereof, polyvinylchloride (PVC), polyvinylidene chloride (PVDC), polyamides (PA), polyurethanes (PU), acrylonitrile butadiene styrene (ABS), polyesters, polycarbonate (PC), rubbers and mixtures thereof.3. Process according to embodiment 1 or 2 wherein said at least one pyrolysis oil PO is manufactured by a pyrolysis reaction from plastic waste and wherein said plastic waste comprises polyalkenes.4. Process according to any one of embodiments 1 to 3 wherein said at least one pyrolysis oil PO comprises a) 5 to 70 wt.-% < 05 hydrocarbons, preferably 40 to 70 wt.-% < 05 hydrocarbons (determined according to ASTM D D5134) and / or b) 5 to 70 wt.-% 05 to 06 hydrocarbons, preferably 25 to 70 wt.-% 05 to 06 hydrocarbons (determined according to ASTM D 5134) and / or c) 0 to 10 wt.-% 08 to 012 hydrocarbons, preferably 0 to 2 wt.-% 08 to 012 hydrocarbons (determined according to ASTM D 5134) and / or d) 0 to 10 wt.-% > 012 hydrocarbons, preferably 0 to 2 wt.-% > 012 hydrocarbons (determined according to ASTM D 5134) and / or e) 5 to 50 wt.-% 06-08 aromatic hydrocarbons, preferably 5 to 20 wt.-% 06-08 aromatic hydrocarbons (determined according to ASTM D 5134) and / or f) 0 to 2 wt.-% styrene, preferably 0 to 0.5 wt.-% styrene (determined according to ASTM D 5134) and / or g) no more than 500 ppmw sulfur, preferably no more than 250 ppmw sulfur (determined according to ASTM 5453 and / or h) no more than 150 ppmw nitrogen, preferably no more than 50 ppmw nitrogen (determined according to ASTM D 6069) and / orI) no more than 50 ppmw chlorine, preferably no more than 10 ppmw chlorine (determined according to ASTM 5291.5. Process according to any one of embodiments 1 to 4 wherein said at least one pyrolysis oil PO hasj) a final boiling point FBP of 100 to 300 °C, preferably of 150 to 250 °C (determined according to EN ISO 3405) and / or k) a density of 0.6 to 0.8 kg / l, preferably of 0.7 to 0.8 kg / l (determined according to ASTM D 4052).6. Process according to any one of embodiments 1 to 5 wherein said at least one pyrolysis oil PO is subjected to at least one upgrading process before provided in step (i).7. Process according to embodiment 6 wherein said at least upgrading process is selected from the group comprising washing, extraction, absorption, adsorption, distillation, hydrotreatment, catalytic cracking, catalytic aromatization and combinations thereof.8. Process according to any one of embodiments 1 to 7 wherein said at least one steam cracking oven SCO comprises at least one coil in which the first feedstock F1 is converted into said effluent E.9. Process according to any one of embodiment 1 to 8 wherein said first cooling unit CU1 is selected from the group comprising shell-and-tube exchanger, tunnel-flow exchanger, double-pipe exchanger, double-pipe-lin- ear exchanger, multi-double-pipe exchanger, and double-pipe-linear exchanger.10. Process according to any one of embodiments 1 to 9 wherein said first quench unit QU1 is selected from the group comprising tangential-injection mixing devices, static mixers, vessels comprising at least one spraynozzle for insertion of said quench oil QO, and counter-flow washers.11 . Process according to any one of embodiments 1 to 10 wherein said cooled effluent CE is fed into said first quench unit QU1 through an inlet 11, said quenching oil QO through an inlet I2 and wherein said stream CE1 leaves said first quench unit QU1 through an outlet 01 and said stream CE2 through an outlet 02.12. Process according to any one of embodiments 1 to 11 wherein said stream CE1 is enriched in 06-08 aromatic hydrocarbons, 02-04 alkenes and 01-04 alkanes compared to said cooled effluent CE.13. Process according to anyone of embodiments 1 to 12 wherein said stream CE2 is depleted in 06-08 aromatic hydrocarbons, 02-04 alkenes and 01-04 alkanes compared to said cooled effluent CE.14. Process according to any one of embodiments 1 to 13 wherein said second quench unit QU2 is selected from the group comprising tangential-injection mixing devices, static mixers, vessels comprising at least one spraynozzle for insertion of said at least one pyrolysis oil PO, and counter-flow washers.15. Process according to any one of embodiments 1 to 14 wherein said at least one quench oil QO is selected from the group comprising or preferably consisting of hydrocarbons or a mixture of hydrocarbons having a boiling point BP which is higher than the temperature T of the cooled effluent CE1.16. Process according to any one of embodiments 1 to 15 wherein said first feedstock F1 is a liquid or a liquified gas, preferably a liquid or liquified gas selected from the group comprising or preferably consisting of naphtha, gas condensates, preferably the 180 to 350 °C cut thereof which is also known as gas oil, hydrocracker bottoms, preferably the 350 to 600 °C cut thereof, a stream BTX which consists of 30 to 50 wt.-% benzene, 10 to 25 wt.-% toluene, 2 to 8 wt.-% xylene, 4 to 9 wt.-% ethyl benzene and less than 45 wt.-% other components, wherein said other components are selected from cyclopentane, cyclopentene, n-hexane, methyl cyclopentane and methyl cyclopentene, and mixtures thereof.17. Process according to any one of embodiments 1 to 16 wherein said cooled effluent CE1 preferably has a temperature in the range of 80 to 140 °C, more preferably 100 to 130 °C and most preferably 105 to 125 °C when entering the second quench unit QU2.18. Process according to any one of embodiments 1 to 17 wherein said at least one pyrolysis oil PO preferably has a temperature in the range of 30 to 90 °C, more preferably 40 to 80 °C and most preferably 50 to 60 °C when entering the second quench unit QU2.19. Process according to any one of embodiments 1 to 18 wherein said stream PO and said stream CE1 are cooled in said second quench unit QU2 and thereby separated into a stream POCE1, said stream POCE1 comprising stream PO1 and said stream CE1, and a stream POCE2, said stream POCE2 comprising said stream PO2 and said stream CE2.20. Process according to any one of embodiments 1 to 19 wherein said second quench unit QU2 comprises at least an inlet I3 and an inlet I4 and an outlet 03 and an outlet 04 and wherein a) said at least one pyrolysis oil PO is fed into said second quench unit QU2 through said inlet I3, b) said cooled effluent CE1 is fed into said second quench unit QU2 through said inlet I4, c) said stream PO1 and said stream CE1a leave said second quench unit CU2 through said outlet 03 as stream POCE1 and d) said stream PO2 and said stream CE1b leave said second quench unit QU2 through said outlet 04 as stream POCE2.21 . Process according to any one of embodiments 1 to 20 wherein said stream PO1 has an initial boiling point IBP (determined according to ASTM D86-23) of not more than 35 °C, preferably of not more than 20 °C and more preferably of not more than 15 °C.22. Process according to any one of embodiments 1 to 21 wherein said stream PO2 comprised in stream POCE2 is enriched in C6-C8 aromatic hydrocarbons compared to stream PO.23. Process according to any one of embodiments 1 to 22 wherein said stream PO comprised in stream POCE2 is depleted in C2-C4 alkenes and depleted in C1 -04 alkanes compared to said stream PO.24. Process according to any one of embodiments 1 to 23 wherein said stream P01 comprised in stream POCE1 is depleted in 06-08 aromatic hydrocarbons compared to stream PO.25. Process according to any one of embodiments 1 to 24 wherein said stream P01 comprised in stream POCE1 is enriched in 02-04 alkenes and enriched in 01-04 alkanes compared to said stream PO.26. Process according to any one of embodiments 1 to 25 wherein said stream P0CE2 is subjected to a 06-08 aromatic hydrocarbons extraction in a 06-08 aromatic hydrocarbon extraction unit AEU, which 06-08 aromatic hydrocarbon extraction unit AEU is downstream of the second quench unit QU2 and optionally fluidically connected to said first outlet 01 of said second quench unit QU2, and a) in which a stream P0CE2a and a stream P0CE2b are separated from said stream P0CE2 and b) wherein said stream P0CE2a is enriched in 06-08 aromatic hydrocarbons compared to said stream P0CE2 and c) wherein said stream P0CE2b is depleted in 06-08 aromatic hydrocarbons compared to said stream P0CE2.27. Process according to any one of embodiments 1 to 26 wherein said stream P01 has a final boiling point FBP (determined according to EN ISO 3405) of no more than 105 °C, preferably of no more than 100 °C and more preferably of no more than 90 °C.28. Process according to any one of embodiments 1 to 27 wherein said stream POCE1 preferably has a temperature of 20 to 50 °C, more preferably 25 to 45 °C and most preferably 30 to 40 °C when leaving the second quench unit QU2.29. Process according to any one of embodiments 1 to 28 wherein said stream POCE2 preferably has a temperature of 65 to 100 °C, more preferably 70 to 95 °C and most preferably 75 to 90 °C when leaving the second quench unit QU2.30. Process according to any one of embodiments 1 to 29 wherein said stream POCE1 is subjected to, preferably in this order, a process sequence comprising the steps compression, acid-gas removal, drying, hydrocarbon fractionating and hydrotreatment in a separation unit SU and thereby separating C2-C4 alkenes in at leastone alkene stream POCEIb and C1-C4 alkanes in at least one further stream POCEIa from said stream P0CE1. Process according to embodiment 30 wherein said stream POCEIa is depleted in C2-C4 alkenes compared to said stream POCE1. Process according to embodiment 30 or 31 wherein at least a portion of said stream POCE2a and / or at least a portion of said stream POCEIa is / are fed into at least one steam cracking oven SCO. Process according to any one of embodiments 1 to 32 wherein said stream POCE1 is subjected to, preferably in this order, a process sequence comprising the steps compression, acid-gas removal, drying, hydrocarbon fractionating and hydrotreatment in a separation unit SU and thereby separating 02-04 alkanes in at least one alkene stream POCEIa and C1-C4 alkenes in at least one further stream POCEIb from said stream POCE1. Process, preferably according to any one of embodiments 1 to 33, comprising the step:- converting the at least one of the C2-C4 alkenes separated from stream POCE1 and / or at least one of the C6-C8 aromatic hydrocarbons separated from stream POCE2 obtainable by or obtained by the process according to any one of embodiments 1 to 33 or a chemical material obtainable by or obtained by the process according to any one of embodiments 1 to 33 to obtain a product PRF1. Process according to embodiment 34, 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; or iii) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition 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.Process according to any one of embodiment 34 or 35, wherein the content of the at least one of the C6-C8 aromatic hydrocarbons separated from stream POCE2 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 wherein the content of the at least one of the C6-C8 aromatic hydrocarbon separated from stream POCE2 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 preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard. Use of at least one pyrolysis oil PC for separation of C6-C8 aromatic hydrocarbons comprised in a cooled cracker effluent CE from C2-C4 alkenes and C1-C4 alkanes also comprised in said cooled cracker effluent CE, wherein said at least one pyrolysis oil PC is manufactured by pyrolysis from plastic waste.

Claims

Claims1. Process for treating a pyrolysis oil in a steam cracking unit, wherein said steam cracking unit comprises a) at least one steam cracking oven SCO, b) a first cooling unit CU1 wherein said first cooling unit CU1 is downstream of and fluidically connected to said at least one cracking oven SCO, c) a first quench unit QU 1, wherein said first quench unit QU1 is downstream of and fluidically connected to said first cooling unit CU1, d) and a second quench unit QU2 wherein said second quench unit QU2 is downstream and fluidically connected to said first quench unit QU1, said process comprising the steps(I) providing a first feedstock F1, a water stream W, a quench oil QO and at least one pyrolysis oil PC, wherein the at least one pyrolysis oil PC is manufactured by pyrolysis from plastic waste and wherein said at least one pyrolysis oil PC comprises 02-04 alkenes and 06-08 aromatic hydrocarbons,(ii) feeding said first feedstock F1 into said at least one steam cracking oven SCO and thereby forming an effluent E which leaves said at least one steam cracking oven SCO,(ill) feeding said effluent E into said first cooling unit CU1 whereby heat is transferred from said effluent E to said water stream W and thereby a cooled effluent CE is formed from said effluent E and wherein said effluent and said water stream W are indirectly contacted in said first cooling unit CU1 with each other,(iv) feeding said cooled effluent CE into said first quench unit QU1 and directly contacting said cooled effluent CE with said quench oil QO in said first quench unit QU1 and thereby separating said cooled effluent CE into a first cooled effluent CE1 and a second cooled effluent CE2 which both leave said first quench unit QU1 wherein the second cooled effluent CE2 comprises said quench oil QO after said quench oil QO was directly contacted with said cooled effluent CE,(v) contacting said at least one pyrolysis oil PC with said first cooled effluent CE1 inside said second quench unit QU2, whereby said at least one pyrolysis oil PC is separated into a stream P01 and a stream P02, whereby said first cooled effluent CE1 is separated into a stream CE1a and a stream CE1b, whereby said stream P01 and said stream CE1a form a stream P0CE1 in said second quench unit QU2, which stream P0CE1 leaves said second quench unit QU2 and whereby said stream P02 and said stream CE1b form a stream P0CE2 in said second quench unit QU2, which stream P0CE2 leaves said second quench unit QU2, said stream P0CE2 comprising 06-08 aromatic hydrocarbons.

2. Process according to claim 1 or 2 wherein said at least one pyrolysis oil PO comprises a) 5 to 70 wt.-% < C5 hydrocarbons, preferably 40 to 70 wt.-% < C5 hydrocarbons (determined according to ASTM D D5134) and / or b) 5 to 70 wt.-% C5 to C6 hydrocarbons, preferably 25 to 70 wt.-% C5 to C6 hydrocarbons (determined according to ASTM D 5134) and / or c) 0 to 10 wt.-% C8 to C12 hydrocarbons, preferably 0 to 2 wt.-% C8 to C12 hydrocarbons (determined according to ASTM D 5134) and / or d) 0 to 10 wt.-% > C12 hydrocarbons, preferably 0 to 2 wt.-% > C12 hydrocarbons (determined according to ASTM D 5134) and / or e) 5 to 50 wt.-% C6-C8 aromatic hydrocarbons, preferably 5 to 20 wt.-% C6-C8 aromatic hydrocarbons (determined according to ASTM D 5134) and / or f) 0 to 2 wt.-% styrene, preferably 0 to 0.5 wt.-% styrene (determined according to ASTM D 5134) and / or g) no more than 500 ppmw sulfur, preferably no more than 250 ppmw sulfur (determined according to ASTM 5453 and / or h) no more than 150 ppmw nitrogen, preferably no more than 50 ppmw nitrogen (determined according to ASTM D 6069) and / orI) no more than 50 ppmw chlorine, preferably no more than 10 ppmw chlorine (determined according to ASTM 5291.

3. Process according to claim 1 or 2 wherein said cooled effluent CE is fed into said first quench unit QU1 through an inlet 11, said quenching oil QO through an inlet I2 and wherein said stream CE1 leaves said first quench unit QU1 through an outlet 01 and said stream CE2 through an outlet 02.

4. Process according to any one of claims 1 to 3 wherein said first feedstock F1 is a liquid or a liquified gas, preferably a liquid or liquified gas selected from the group comprising or preferably consisting of naphtha, gas condensates, preferably the 180 to 350 °C cut thereof which is also known as gas oil, hydrocracker bottoms, preferably the 350 to 600 °C cut thereof, a stream BTX which consists of 30 to 50 wt.-% benzene, 10 to 25 wt.-% toluene, 2 to 8 wt.-% xylene, 4 to 9 wt.-% ethyl benzene and less than 45 wt.-% other components, wherein said other components are selected from cyclopentane, cyclopentene, n-hexane, methyl cyclopentane and methyl cyclopentene, and mixtures thereof.

5. Process according to any one of claims 1 to 4 wherein said at least one pyrolysis oil PO preferably has a temperature in the range of 30 to 90 °C, more preferably 40 to 80 °C and most preferably 50 to 60 °C when entering the second quench unit QU2.

6. Process according to any one of claims 1 to 5 wherein said stream PO and said stream CE1 are cooled in said second quench unit QU2 and thereby separated into a stream POCE1, said stream POCE1 comprisingstream PO1 and said stream CE1, and a stream POCE2, said stream POCE2 comprising said stream P02 and said stream CE2.

7. Process according to any one of claims 1 to 6 wherein said second quench unit QU2 comprises at least an inlet I3 and an inlet I4 and an outlet 03 and an outlet 04 and wherein a) said at least one pyrolysis oil PO is fed into said second quench unit QU2 through said inlet I3, b) said cooled effluent CE1 is fed into said second quench unit QU2 through said inlet I4, c) said stream P01 and said stream CE1a leave said second quench unit CU2 through said outlet 03 as stream P0CE1 and d) said stream P02 and said stream CE1b leave said second quench unit QU2 through said outlet 04 as stream P0CE2.

8. Process according to any one of claims 1 to 7 wherein said stream P01 has an initial boiling point IBP (determined according to ASTM D86-23) of not more than 35 °C, preferably of not more than 20 °C and more preferably of not more than 15 °C.

9. Process according to any one of claims 1 to 8 wherein said stream PO1 has a final boiling point FBP (determined according to EN ISO 3405) of no more than 105 °C, preferably of no more than 100 °C and more preferably of no more than 90 °C.

10. Process according to any one of claims 1 to 9 wherein said stream PO2 comprised in stream POCE2 is enriched in C6-C8 aromatic hydrocarbons compared to stream PO.

11. Process according to any one of claims 1 to 10 wherein said stream PO1 comprised in stream POCE1 is enriched in C2-C4 alkenes and enriched in C1 -04 alkanes compared to said stream PO.

12. Process according to any one of claims 1 to 11 wherein said stream POCE2 preferably has a temperature of 65 to 100 °C, more preferably 70 to 95 °C and most preferably 75 to 90 °C when leaving the second quench unit QU2.

13. Process according to any one of claims 1 to 12 wherein said stream POCE2 is subjected to a 06-08 aromatic hydrocarbons extraction in a 06-08 aromatic hydrocarbon extraction unit AEU, which 06-08 aromatic hydrocarbon extraction unit AEU is downstream of the second quench unit QU2 and optionally fluidically connected to said first outlet 01 of said second quench unit QU2, and a) in which a stream POCE2a and a stream POCE2b are separated from said stream POCE2 and b) wherein said stream POCE2a is enriched in 06-08 aromatic hydrocarbons compared to said stream POCE2 andc) wherein said stream POCE2b is depleted in C6-C8 aromatic hydrocarbons compared to said stream POCE2.

14. Process according to any one of claims 1 to 13, comprising the step:- converting the at least one of the C2-C4 alkenes separated from stream POCE1 and / or at least one of the C6-C8 aromatic hydrocarbons separated from stream POCE2or a chemical material obtainable by or obtained by the process according to any one of claims 1 to 13 to obtain a product PRF1 .

15. Process according to claim 14, wherein the product PRF1 is selected from:I) building block or monomer; orII) polymer, preferably polymer A, polymer composition, preferably polymer composition A, or polymer product, preferably polymer product A; or ill) cleaning polymer, cleaning surfactant, descaling compound, cleaning biocide or composition 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.

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