Process for manufacturing aldehydes and alcohols from plastic waste

Abstract

The present invention relates to a process for manufacturing aliphatic C3−C5 aldehydes, aliphatic C9−C13 alcohols from plastic waste and chemical products based on aliphatic C3−C5 aldehydes and aliphatic C9−C13 alcohols from plastic waste and a chemical plant for providing C2−C4 olefins and syngas which are used in said process. 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 partial oxidation in at least one gasifier. 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

[0001] 240987W001

[0002] Process for manufacturing aldehydes and alcohols from plastic waste

[0003] Technical area

[0004] The present invention relates to a process for manufacturing aliphatic C3-C5 aldehydes, aliphatic C9-C13 alcohols from plastic waste and chemical products based on aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols from plastic waste.

[0005] Background of the invention

[0006] Aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols are important intermediate products in the chemical industry from which for example aliphatic alcohols and organic acids are manufactured. Such alcohols and acids can then be used as building blocks and / or precursors in the manufacture of solvents, plasticizers, lubricants, and surfactants.

[0007] The usual starting materials for the manufacture of aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols are C2-C4 olefins and syngas (gas mixture comprising CO and H2) which are manufactured from fossil sources such as processed crude oil and natural gas. Aliphatic C3-C5 aldehydes are then manufactured from C2-C4 olefins and syngas by a hydroformylation reaction which is also known as oxo-synthesis. Aliphatic C9-C13 alcohols are manufactured from oligomers of C2-C4 olefins, such as C8 olefins and C12 olefins, and syngas by a hydroformylation reaction. The aldehydes obtained as primary reaction product of the hydroformylation reaction from such oligomers of C2-C4 olefins and syngas usually further react to the corresponding aliphatic C9-C13 alcohols. Hence, aliphatic C9-C13 aldehydes are usually not isolated.

[0008] Amid global warming and climate change, it has become a global incentive to reduce fossil emissions. By utilizing recycled feedstock (e.g., plastic waste), the chemical industry can significantly reduce its dependence on virgin resources such as fossil sources, leading to a decrease in resource depletion and environmental pollution.

[0009] 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)”.

[0010] 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 240987W001

[0011] 2 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.

[0012] 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.

[0013] It is an objective of the present invention to provide a process for manufacturing C2-C4 olefins and / or a mixture of CO and H2 from plastic waste.

[0014] It is a further objective if the present invention to provide a process for manufacturing of aliphatic C3-C5 aldehydes from plastic waste.

[0015] It is a further objective if the present invention to provide a process for manufacturing of aliphatic C9-C13 alcohols from plastic waste.

[0016] It is a further objective if the present invention to provide a process for manufacturing aliphatic alcohols and carboxylic acids from plastic waste.

[0017] It is a further objective of the present invention to provide aliphatic alcohols and carboxylic acids, manufactured from plastic waste for manufacture of solvents, plasticizers, lubricants, and surfactants.

[0018] It is a further 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.

[0019] 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. 240987W001

[0020] 3

[0021] 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.

[0022] 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.

[0023] 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.

[0024] Summary of the invention

[0025] These objectives are solved by a process for manufacturing aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols from C2-C4 olefins and syngas comprising the steps a) providing a C2-C4 olefin or an oligomer thereof, b) providing a mixture of CO and H2, c) contacting the C2-C4 olefin or oligomer thereof provided in step a) and the mixture of CO and H2 provided in step b), preferably in the presence of at least one catalyst, and thereby forming an aliphatic C3-C5 aldehyde or an aliphatic C9-C13 alcohol, wherein the process, prior to step a), also comprises the steps of

[0026] (i) providing a feed stream S1 , wherein said feed stream S1 comprises or preferably consists of plastic waste,

[0027] (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,

[0028] (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, 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,

[0029] (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', and converting said stream S5 by a partial oxidation process in at least one gasifier G into a mixture of CO and H2, 240987W001

[0030] 4

[0031] (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",

[0032] (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,

[0033] (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,

[0034] (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, and

[0035] (ix) converting at least one of the streams selected from the group consisting of S6a, S8 and S9 by a steam cracking process in at least one steam cracking unit SCU into C2-C4 olefins and, optionally converting at least a portion of said C2-C4 olefins into oligomers thereof.

[0036] 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 directly or indirectly fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2, further comprising h) at least one gasifier G, said at least on gasifier G downstream of and directly or indirectly fluidically connected to the separation unit SU and / or at least one steam cracking unit SCU, said at least one steam cracking unit downstream of and directly or indirectly fluidically connected to at least one of the members selected from the 240987W001

[0037] 5 group consisting of at least one first condensation unit CU1, at second condensation unit CU2 and the optional at least one mixing unit MU.

[0038] The process according to the present invention provides the following advantages:

[0039] Aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols can be manufactured from plastic waste as feedstock and have therefore a recycle-content of 100 % in case all C2-C4 olefin provided in step a) and all the mixture of CO and H2 (“synthesis gas” / “syngas”) provided in step b) is manufactured by steps (i) to (ix).

[0040] Aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols having a recycle-content of less than 100 % can also be manufactured by the process according to the present invention in case not all C2-C4 olefin provided in step a) and / or not all syngas provided in step b) is / are manufactured by steps (i) to (ix) and instead at least a portion of the C2-C4 olefin and / or the oligomer thereof provided in step a) and / or at least a portion of the syngas provided in step b) is / are manufactured e.g., from fossil feedstocks. Hence, the process according to the present invention also enables manufacture of aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols with a desired recycle-content of less than 100 %.

[0041] The aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols manufactured from plastic waste and therefore having a recycle-content can be used as the starting materials for manufacturing aliphatic alcohols and carboxylic acids therefrom which, accordingly, also have a recycle-content of up to 100 % in case the aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols are manufactured from C2-C4 olefins or oligomers thereof provided in step a) and syngas provided in step b) which are both manufactured by steps (i) to (ix). Aliphatic alcohols and carboxylic acids having a recycle-content of less than 100 % can be manufactured from aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols having a recycle-content of less than 100 %. Accordingly, the process according to the present invention also enables manufacture of aliphatic alcohols and organic acids therefrom with a desired recycle-content of less than 100 %.

[0042] The aliphatic alcohols and carboxylic acids manufactured from plastic waste and therefore having a recycle-content can be used as the feedstock for manufacturing products, which, accordingly, have also a recycle-content of up to 100 % in case all aliphatic alcohols and carboxylic acids are manufactured from C2-C4 olefins or oligomers thereof provided in step a) and syngas provided in step b) are manufactured by steps (i) to (ix) via aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols. Products having a recycle-content of less than 100 % can be manufactured from aliphatic alcohols and carboxylic acids having a recycle-content of less than 100 %. Accordingly, the process according to the present invention also enables manufacture of products with a desired recycle-content of less than 100 %.

[0043] In case the plastic waste from which products having a recycle-content is produced comprises products, the process according to the present invention is a closed recycling loop for products. 240987W001

[0044] 6

[0045] In manufacture of aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols manufactured from plastic waste according to steps (i) to (ix) undesired polymerization and fouling is suppressed.

[0046] 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 (physically 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.

[0047] 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.

[0048] 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.

[0049] 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.

[0050] 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.

[0051] 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 240987W001

[0052] 7 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.

[0053] A feed stream 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 low boiling fraction of the full range pyrolysis oil requires to be condensed in condensation units. Thereby further energy can be saved. Said low boiling fraction is suited for production of C2-C4 olefins by steam cracking in at least one steam cracking unit.

[0054] Figures

[0055] Figure 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.

[0056] 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.

[0057] 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.

[0058] Detailed description of the invention

[0059] The 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.

[0060] Definitions:

[0061] 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 240987W001

[0062] 8 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 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”).

[0063] 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.

[0064] 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.

[0065] 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. 240987W001

[0066] 9

[0067] 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.

[0068] 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.

[0069] 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.

[0070] 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.

[0071] 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 about 200 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 240987W001

[0072] 10 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).

[0073] 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).

[0074] 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:

[0075] 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. 240987W001

[0076] 11

[0077] 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.

[0078] 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 .

[0079] 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 .

[0080] 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 240987W001

[0081] 12 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.

[0082] 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.

[0083] 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, mixtures thereof, and mixtures thereof further comprising at least one further oil FO. 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.

[0084] 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.

[0085] 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 240987W001

[0086] 13 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):

[0087] 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.

[0088] 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):

[0089] 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.

[0090] 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) 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 340 to 380 °C (determined according to ASTM D86-23):

[0091] 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. 240987W001

[0092] 14

[0093] 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.

[0094] 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.

[0095] 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.

[0096] 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.

[0097] 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.

[0098] Said second intermediate stream S4' is depleted in C11 -C21+ hydrocarbons compared to said first intermediate stream S4.

[0099] 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, liqu id / gas coalescers, and combinations thereof.

[0100] Optionally, the at least one quench unit QU and said separation unit SU are combined in a quench and separation unit QSU. 240987W001

[0101] 15

[0102] The liquid high boiling fraction S5 is then used as a feedstock or co-feedstock for a partial oxidation reaction in at least one gasifier G in which said stream S5 is converted into a mixture of CO and H2 (also known as “synthesis gas” or “syngas”). Such partial oxidation reactions are known in the art and are for example disclosed in WO 2022 / 200532 A1 and R. Reimert et al., Ulmann's Encyclopedia of Industrial Chemistry, Vol. 16, p. 446 to 482, 2012, Wiley-VCH Verlag GmbH & Co. KGaA, Weinheim (DOI: 10.1002 / 14356007.o12). 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.

[0103] Suitable co-feedstocks for the liquid high boiling fraction S5 in said partial oxidation process in at least one gasifier G 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.

[0104] At least a portion of the mixture of CO and H2 made from stream S5 and optionally at least one further co-feedstock in at least one gasifier G by partial oxidation is then provided in step b).

[0105] 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.

[0106] 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.

[0107] Said medium boiling fraction S6 comprises 06-020 hydrocarbons. Said medium boiling fraction S6 has a final boiling point FBP (determined according to ASTM D86-23) of lesson more than 380 °C.

[0108] 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. 240987W001

[0109] 16

[0110] 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.

[0111] 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.

[0112] A water stream S10 is optionally also separated from the third intermediate stream S4" in the second condensation unit CU2.

[0113] 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.-%.

[0114] 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).

[0115] 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.

[0116] 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). 240987W001

[0117] 17

[0118] 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.

[0119] In step (ix) of the process according to the present invention, 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 in at least one steam cracking unit SCU. Optionally, said stream(s) are upgraded by at least one upgrading process before fed into a steam cracking unit. Said at least one optional upgrading process is preferably 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 at least one steam cracking unit SCU. Steam cracking units SCU 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 (DOI: 10.1002 / 14356007. a10_045.pub3). The main reaction products of said steam cracking process in at least one steam cracking unit SCU are C2-C4 olefins of which at least a portion is then provided in step a), preferably after separating said C2-C4 olefins into C2 olefins, C3 olefins and C4 olefins and, optionally, after forming an oligomer thereof.

[0120] In step a) of the process according to the present invention, a C2-C4 olefin or an oligomer thereof is provided. At least a portion of the C2-C4 olefin or oligomer thereof provided in step a) is manufactured by steps (i) to (ix). The C2-C4 olefin is selected from the group consisting of ethylene, propylene, 1 -butene, and 2-butene. C2-C4 olefins manufactured by steps (i) to (ix) have a recycle-content of 100 %.

[0121] Optionally, an oligomer of the C2-C4 olefin is provided in step a). Such oligomers can be manufactured by dimerization or trimerization of C2-C4 olefins. Condensation products of the C2-C4 olefin preferred for step a) comprise C8 to C12 olefins. The condensation products of C2-C4 olefins are preferably selected from the group consisting of di-n-butene, tri-n-butene, 2,4,4-trimethyl-1 -pentene, 2,4,4-trimethyl-2-pentene and dodec-1-ene. Di-n- butene and tri-n-butene are C8 alkene and C12 alkene isomers, respectively, which comprise branched C8 isomers 240987W001

[0122] 18 and, respectively, C12 isomers. Oligomers of C2-C4 olefins manufactured by steps (i) to (ix) have a recycle-content of 100 %.

[0123] The manufacture of oligomers of C2-C4 olefins, particularly of condensation of C4 olefins to 08 olefins in the presence of a solid acid catalyst is disclosed for example in US 2014 / 0128652 A1. Sold acid catalysts include silica- alumina, silica-magnesia, silica-boria, alumina-boria, chlorinated alumina, fluorinated alumna, synthetic zeolites and the like. Another method for manufacture of oligomers of 02-04 olefins, particularly of condensation of 04 olefins to 08 olefins using a nickel oxide catalyst is disclosed in EP 1171413 B1. The manufacture of oligomers of 02-04 olefins, particularly condensation of 04 olefins to 012 olefins is disclosed for example in WO 01 / 36356 A2. 04 olefins are contacted with a heterogeneous catalyst comprising a metal such as nickel at an elevated temperature and thereby, a 012 olefin is formed. The 012 olefins can be further converted in step c) in the presence of a mixture of CO and H2.

[0124] Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the 02-04 olefins or oligomers thereof provided in step a) are 02-04 olefins or oligomers thereof manufactured from a nonfossil feedstock. Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the 02-04 olefins or oligomers thereof provided in step a) are manufactured by steps (i) to (ix).

[0125] 02-04 olefins can be for example manufactured from fossil feedstocks such as naphtha by steam cracking processes or by fluid catalytic cracking processes.

[0126] Preferably, the feed stream S1 provided in step (i) comprises at least one product which can be made from the aliphatic 03-05 aldehydes, aliphatic 09-013 alcohols obtained by the process according to any claims of the present invention. Thereby, a closed recycling-loop can be archived by the process according to the present invention.

[0127] In step b) of the process according to the present invention, syngas is provided.

[0128] The syngas comprises, preferably consists of CO and H2, more preferably of CO and H2 in a molar ratio of 30 : 70 to 50 : 50, most preferably of CO and H2 in a molar ratio of 35 : 65 to 45 : 55. Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the syngas provided in step b) is syngas manufactured from a non-fossil feedstock. Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the syngas provided in step b) is manufactured by a partial oxidation process in at least one gasifier G from stream S5 separated in step (iv). Syngas can be for example manufactured from fossil feedstocks such as heavy fractions of crude oil processing by partial oxidation or steam reforming of natural gas. 240987W001

[0129] 19

[0130] Optionally, the mixture of CO and H2 manufactured from stream S5 is then separated into CO and said H2 and only CO or H2 is then provided in step b) together with CO or H2 manufactured from another feedstock than feed stream S1 provided in step (i).

[0131] Additional hydrogen can be added to the syngas in case the syngas provided in step b) has a molar ratio CO : H2 of > 50 : 50. The additional hydrogen can be in principle hydrogen generated from any known source and by any known method. Preferably, such additional hydrogen is “green hydrogen” which is generated for example by electrolysis of water using electricity generated from renewable energy sources (e.g., solar energy, wind energy, tidal energy, and nuclear energy) and / or low-carbon energy sources and / or formed by a methane pyrolysis, preferably a methane pyrolysis using at least partially methane from a renewable source. Methane from a renewable source comprises biomethane. Additional CO can be added to the syngas in case the syngas provided in step b) has a molar ratio CO : H2 of < 30 : 70. The additional CO can be in principle CO generated and / or separated from any known source and by any known method.

[0132] In step c) of the process according to the present invention, a C2-C4 olefin is contacted with syngas whereby an aliphatic C3-C5 aldehyde is formed, or a condensation product of a C2-C4 olefin provided in step a) is contacted with syngas whereby an aliphatic C9-C13 alcohol is formed. Preferably, the C2-C4 olefin and syngas are contacted on step c) in the presence of at least one catalyst.

[0133] Aliphatic C3-C5 aldehydes are manufactured in step c) from C2-C4 olefins, CO and H2 by hydroformylation. The aliphatic C3-C5 aldehyde is preferably selected from the group consisting of propanal, 1 -butanal, 2-methylpropanal, 1 -pentanal, and 2-methylbutanal. Accordingly, propanal is formed by an oxo-synthesis from ethene, CO and H2; n- butanal and i-butanal or formed by an oxo-synthesis from propene, CO and H2; n-pentanal and 2-methylbutyral are formed by an oxo-synthesis from 1 -butene and / or 2-butene, CO and H2; 3-methylpenanal is formed by an oxo- synthesis from isobutene, CO and H2.

[0134] Hydroformylation also known as “oxo-process” and “oxo-synthesis” is an important large-scale industrial process for preparing aldehydes from olefins, CO and H2. These aldehydes can optionally be hydrogenated with hydrogen in the same operation or subsequently in a separate hydrogenation step, to produce the corresponding alcohols. Hydroformylation is carried out in the presence of catalysts which are preferably homogeneous catalyst comprising at least one metal. Said catalyst is preferably homogeneously dissolved in the reaction medium. Catalysts used are preferably carbonyl complexes of metals of transition group VIII, in particular cobalt, rhodium, iridium, palladium, platinum or ruthenium, which may be unmodified or modified with, for example, amine-containing or phosphine- containing ligands. A summarizing account of the processes practiced on a large scale in industry is found in J. Falbe, "New Syntheses with Carbon Monoxide", Springer Verlag 1980, p. 162 ff.

[0135] While short-chain olefins with up to 5 carbon atoms are currently predominantly hydroformylated using ligand- modified rhodium carbonyls as the catalyst, cobalt remains the dominant catalytically active central atom for longer- 240987W001

[0136] 20 chained olefins such as oligomers of short-chain olefins, e.g., isooctane and dodecene. This is due, firstly, to the high catalytic activity of the cobalt carbonyl catalyst irrespective of the position of the olefinic double bonds, the branch structure and the purity of the olefin to be reacted. Secondly, the cobalt catalyst can be separated off from the hydroformylation products and recycled into the hydroformylation reaction relatively easily. Additionally, catalyst losses during working up can be tolerated more easily owing to the lower price of cobalt.

[0137] In one customary process for separating off and recycling the cobalt catalyst, the organic phase of the reactor effluent is freed of cobalt carbonyl complexes by treatment with oxygen or air in the presence of weakly acidic water (cf. DE 24 04 855). In the treatment, the cobalt catalyst is destroyed by oxidation and the central atom is formally converted from the oxidation state -1 to +2 and can then be removed by extraction with the aqueous solution (decobaiting). The catalyst complex required for hydroformylation can be re-formed from the cobalt(ll) salt solution by reaction with carbon monoxide and hydrogen (carbonyl formation). The re-formed cobalt catalyst is then extracted from the aqueous phase with an organic phase, preferably the olefin to be hydroformylated (catalyst extraction). Besides the olefin, the reaction products and by-products of the hydroformylation can also be used for catalyst extraction. The olefins loaded with the cobalt catalyst are then hydroformylated in a reactor at elevated pressure and elevated temperature (olefin hydroformylation).

[0138] The pressure during synthesis C3-C5 aldehydes from C2-C4 olefins, CO and H2preferably ranges between about 10 bar to about 20 bar or up to about 100 bar. The temperature ranges during synthesis from about 60 °C to about 130 °C. Preferably, the at least one catalyst comprises rhodium as metal. Catalysts having the general formula [Rh(CO)PR3)3] wherein R = CeHs or S-Ceb SOsNa are most preferred. Further details of the manufacture of aliphatic C3-C5 aldehydes from C2-C4 olefins, CO and H2by an oxo-synthesis are for example disclosed in H. Bahrmann, H. Basch, G. D. Frey, Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Oxo Synthesis”, pages 1 to 8, 2013 and the references cited therein.

[0139] The manufacture of aliphatic C9 aldehydes and aliphatic C9 alcohols from C8 olefins is for example described in WO 2021 / 160448 A1. The manufacture of aliphatic C13 aldehydes and aliphatic C13 alcohols from C12 olefins in the presence of cobalt catalysts is for example described in WO 01 / 36356 A2. Aliphatic C9-C13 alcohols formed in step c) from C8 olefins provided in step a) comprise isomeric nonanols. Aliphatic C9-C13 alcohols formed in step c) from C12 olefins provided in step a) comprise isomeric tridecanols. Aliphatic C9-C13 alcohols are preferably formed from C8 to C12 olefins and syngas by a high-pressure reaction in the presence of a cobalt catalyst. The intermediate aliphatic 09-013 aldehydes are usually not isolated. Hence, the aliphatic 09-013 alcohols are directly obtained by such processes. The pressure during the synthesis preferably ranges from about 50 bar to about 350 bar and the temperature ranges from about 100 °C to about 200 °C. Such high-pressure oxo-processes in the presence of a cobalt catalyst are for example disclosed in H. Bahrmann, H. Basch, G. D. Frey, Ullmann's Encyclopedia of Industrial Chemistry, Chapter “Oxo Synthesis”, pages 1 to 8, 2013 and the references cited therein. 240987W001

[0140] 21

[0141] In optional step d1), the aliphatic C3-C5 aldehyde formed in step c) is further converted into an aliphatic alcohol, preferably by a hydrogenation reaction or two different aliphatic C3-C5 aldehydes of which at least one was formed in step c) are further converted into an aliphatic alcohol by a hydrogenation reaction. The aliphatic C3-C5 alcohol formed in step d 1 ) from one aliphatic C3-C5 aldehyde formed in step c) is preferably selected from the group consisting of 1 -propanol, 2-propanol, 1-butanol, 2-methylpropanol, 1-pentanol, 2-methylbutanol, and 3-methylbutanol. The aliphatic alcohol formed in step d1) from two aliphatic C3-C5 aldehydes of which at least one was formed in step c) is preferably selected from the group consisting of 2-propylheptanol and 2-ethylhexanol. The synthesis of alcohols from aldehydes is for example described in J. Falbe, H. Bahrmann, W. Lipps, D. Mayer, G. D. Frey, Ullmann's Encyclopedia of Industrial Chemistry, chapter “Alcohols, Aliphatic”, 2013, pages 5 to 6 and references cited therein. Another method for converting C3 to C13 aldehydes into aliphatic alcohols is described in WO 2018 / 210720 A1 . Said aldehydes are contacted with a catalyst containing copper oxide and aluminium oxide at a temperature of 150 °C to 300 °C and a pressure of 20 bar to 300 bar in the presence of hydrogen. Thereby, alcohols are formed from the respective aldehydes.

[0142] At least a portion of the aliphatic C3-C5 aldehyde provided in in optional step d1) as starting material is manufactured in step c) from at least a portion of the C2-C4 olefin and / or syngas manufactured by the steps (i) to (ix) (C2-C4 olefin) and / or steps (i) to (iv) (syngas). In case not all the C2-C4 olefin and / or syngas is manufactured by the steps (i) to (ix) and / or steps (i) to (iv), respectively, the remaining C2-C4 olefin and / or syngas is manufactured from other feedstocks than feed stream S1 provided in step (i) and / or by other manufacturing methods.

[0143] Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the C2-C4 olefin and / or syngas used for manufacture of the at least one aliphatic C3-C5 aldehyde provided in optional step d 1 ) is / are manufactured from a non-fossil feedstock. Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the at least one aliphatic C3-C5 aldehyde and / or syngas used for manufacture of the aliphatic C3-C5 aldehyde provided in optional step d 1 ) is formed in step c).

[0144] The process according to the present invention optionally comprises the further step d2) converting the aliphatic C3-C5 aldehyde formed in step c) or the aliphatic alcohol formed in optional step d 1 ) or the aliphatic C9-C13 alcohols formed in step c) into a carboxylic acid.

[0145] The carboxylic acid formed in optional step d2) is preferably selected from the group consisting of propionic acid, n- butanoic acid, n-pentanoic acid, 2-methylpropanoic acid, 2-methylbutanoic acid, 3-methylbutanoic acid, 2,2- dimethylpropanoic acid, 2-ethylhexanoic acid, and 2-propylheptanoic acid. Carboxylic acids can be formed in optional step d2) with an oxidation of the corresponding aldehyde by air or oxygen with or without a catalyst. Preferably, the oxidation is in liquid phase without a solvent. The oxidation can also be a two-phase oxidation (gas-liquid) with a catalyst in the liquid phase. Suitable catalysts comprise salts of metals selected from the group comprising cerium, cobalt, chromium, copper, iron, manganese, molybdenum, nickel, or vanadium. Carboxylic acids can be formed in optional step d2) from aliphatic alcohol formed in optional step d1) or the aliphatic C9-C13 alcohols formed in step c) 240987W001

[0146] 22 by alkali fusion as a dehydrogenation reaction with NaOH or NaOH / KOH mixtures at a temperature of about 250 °C to about 350 °C.

[0147] At least a portion of aliphatic C3-C5 aldehyde formed in step c) or the aliphatic alcohol formed in optional step d1) or the aliphatic C9-C13 alcohols provided in optional step d2) are formed in step c). Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the aliphatic C3-C5 aldehydes formed in step c) or the aliphatic alcohols formed in optional step d 1 ) or the aliphatic C9-C13 alcohols formed in step c) which are converted in optional step d2) is / are manufactured from a non-fossil feedstock. Preferably, at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the aliphatic C3-C5 aldehydes formed in step c) or the aliphatic alcohols formed in optional step d 1 ) or the aliphatic C9-C13 alcohols formed in step c) which are converted in optional step d2) is / are manufactured from the C2-C4 olefin and / or oligomer thereof and / or the mixture of CO and H2 manufactured in steps (i) to (ix) and / or steps (i) to (iv), respectively. The synthesis of carboxylic acids from aliphatic aldehydes by oxidation is for example described in J. Kubitschke, H. Lange, H. Strunz, Ullmann's Encyclopedia of Industrial Chemistry, chapter “Carboxylic Acids, Aliphatic” 2014, pages 5 to 6 and references cited therein.

[0148] Preferred products which can be made from the of the aliphatic C3-C5 aldehydes formed in step c) or the aliphatic alcohols formed in optional step d 1 ) or the aliphatic C9-C13 alcohols formed in step c) or carboxylic acids formed in optional step d2) comprise solvents, plasticizers, lubricants, and surfactants. Some examples of educts and corresponding products are given below: propionic acid: silage additives, animal nutrition; n-butanol: solvent, acrylic ester, butyl acetate; ethylhexanol: plasticizer, acrylic esters; ethylhexane acid: intermediates; trimethylolpropan: polymers, lubricants, paint raw materials; aliphatic C9 alcohols: plasticizer, (non-ionic / anionic) surfactants; aliphatic C9 carboxylic acids: lubricants; 2-propylheptanol: plasticizer, (non-ionic / anionic) surfactants; aliphatic C13 alcohols: (non-ionic / anionic) surfactants, plasticizer.

[0149] 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, 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 , 240987W001

[0150] 23 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 directly or indirectly fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2, further comprising h) at least one gasifier G, said at least on gasifier G downstream of the separation unit SU and directly or indirectly fluidically connected to the separation unit SU and / or at least one steam cracking unit SOU, said at least one steam cracking unit downstream of and directly or indirectly fluidically connected to at least one of the members selected from the group consisting of at least one first condensation unit CU1, at second condensation unit CU2 and the optional at least one mixing unit MU.

[0151] 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.

[0152] The at least one gasifier G is downstream of and directly or indirectly fluidically connected to the at least one separation unit SU. The at least one gasifier G is preferably an entrained flow gasifier. Such entrained flow gasifiers are particularly suited for stream S5 as (co-) feedstock. In case the at least one gasifier G and the separation unit SU are indirectly fluidically connected to each other, at least one further means such as a storage tank and / or a mixing tank in which stream S5 is mixed with at least one co-feedstock can be in between located between said at least one gasifier G and said at least one separation unit SU.

[0153] 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 240987W001

[0154] 24 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.

[0155] 1 . Process for manufacturing aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols from C2-C4 olefins and syngas comprising the steps a) providing a C2-C4 olefin or an oligomer thereof, b) providing a mixture of CO and H2, c) contacting the C2-C4 olefin or oligomer thereof provided in step a) and the mixture of CO and H2provided in step b), preferably in the presence of at least one catalyst, and thereby forming an aliphatic C3-C5 aldehyde or an aliphatic C9-C13 alcohol, wherein the process, prior to step a), also comprises the steps of

[0156] (i) providing a feed stream S1 , wherein said feed stream S1 comprises or preferably consists of plastic waste,

[0157] (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,

[0158] (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,

[0159] (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', and converting said stream S5 by a partial oxidation process in at least one gasifier G into a mixture of CO and H2,

[0160] (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",

[0161] (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 240987W001

[0162] 25 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,

[0163] (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,

[0164] (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 and

[0165] (ix) converting at least one of the streams selected from the group consisting of S6a, S8 and S9 by a steam cracking process in at least one steam cracking unit SCU into C2-C4 olefins and, optionally, converting at least a portion of said C2-C4 olefins into oligomers thereof.

[0166] 2. Process according to embodiment 1 wherein the C2-C4 olefin provided in step a) is selected from the group consisting of ethylene, propylene, 1 -butene, trans-2-butene and cis-2-butene.

[0167] 3. Process according to embodiment 1 or 2 wherein the oligomer of C2-C4 olefin provided in step a) is selected from the group consisting of 2,4,4-trimethyl-1 -pentene, 2,4,4-trimethyl-2-pentene and dodec-1-ene.

[0168] 4. Process according to any one of embodiments 1 to 3 wherein the mixture of CO and H2 provided in step b) has a molar ratio CO : H2 of 30 : 70 to 50 : 50, most preferably of 35 : 65 to 45 : 55.

[0169] 5. Process according to any one of embodiments 1 to 4 wherein the aliphatic C3-C5 aldehyde formed in step c) is selected from the group consisting of propanal, 1-butanal, 2-butanal, 1 -pentanal, and 2-methylbutanal.

[0170] 6. Process according to any one of embodiments 1 to 5 wherein the aliphatic C9-C13 alcohol formed in step c) is selected from the group consisting of 3,5,5-trimethylhexane-1-ol, dimethyl-1 -heptanole, methyl-1-octanolen, 1 -tridecanole, 2-tridecanole, 3-tridecanole, 4-tridecanole, 5-tridecanole, 6-tridecanole, 7-tridecanole and isomeric mixtures of tridecanole.

[0171] 7. Process according to any one of embodiments 1 to 6 wherein preferably at least 2.5 wt.-%, more preferably at least 5.0 wt.-%, most preferably 7.5 wt.-% of the C2-C4 olefin or the oligomer thereof provided in step a) is manufactured by steps (i) to (ix).

[0172] 8. Process according to any one of embodiments 1 to 7 wherein preferably at least 2.5 wt.-%, more preferably at least 5.0 wt.-%, most preferably 7.5 wt.-% of the mixture of CO and H2provided in step b) is manufactured by steps (i) to (iv). 240987W001

[0173] 26

[0174] 9. Process according to any one of embodiments 1 to 8 wherein the at least one catalyst in step c) is a homogeneous catalyst comprising at least one metal.

[0175] 10. Process according to any one of embodiments 1 to 9 wherein the at least one catalyst in step c) comprises at least one metal which is selected from the group consisting of cobalt, rhodium, iridium, palladium, platinum, and ruthenium.

[0176] 11. Process according to any one of embodiments 1 to 10 wherein the at least one catalyst comprises one metal which is cobalt or rhodium.

[0177] 12. Process according to any one of embodiments 1 to 11 wherein the at least one catalyst in step c) is preferably a homogeneous catalyst, more preferably a homogeneous catalyst comprising at least one metal selected from the group consisting of cobalt, rhodium, iridium, palladium, platinum, and ruthenium and most preferably a homogeneous catalyst comprising at least one metal selected from the group consisting of cobalt and rhodium.

[0178] 13. Process according to any of embodiments 1 to 12 comprising the further step d1) converting the aliphatic C3-C5 aldehyde formed in step c) into an aliphatic C3-C5 alcohol or two different aliphatic C3-C5 aldehydes of which at least one was formed in step c) into an aliphatic alcohol and / or d2) converting the aliphatic C3-C5 aldehyde formed in step c) or the aliphatic alcohol formed in optional step d1) or the aliphatic C9-C13 alcohols formed in step c) into a carboxylic acid.

[0179] 14. Process according to embodiment 13 wherein the aliphatic C3-C5 alcohol formed in step d1) is selected from the group consisting of 1 -propanol, 2-propanol, 1 -butanol, 2-methylpropanol, 1 -pentanol, 2-methylbutanol, and 3-methylbutanol.

[0180] 15. Process according to embodiment 13 wherein the aliphatic alcohol formed in step d1) from two different aliphatic C3-C5 aldehydes of which at least one was formed in step c) is selected from the group consisting of 2-propylheptanol and 2-ethylhexanol.

[0181] 16. Process according to embodiment 13 wherein the aliphatic C3-C5 alcohol formed in step d1) is selected from the group consisting of 1 -propanol, 2-propanol, 1 -butanol, 2-methylpropanol, 1 -pentanol, 2-methylbutanol, and 3-methylbutanol. 240987W001

[0182] 27

[0183] 17. Process according to embodiment 13 wherein the aliphatic alcohol formed in step d1) from two different aliphatic C3-C5 aldehydes of which at least one was formed in step c) is selected from the group consisting of 2-propylheptanol and 2-ethylhexanol.

[0184] 18. Process according to any one of embodiment 13 to 17 wherein at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the C2-C4 olefin and / or syngas used for manufacture of the at least one aliphatic C3-C5 aldehyde provided in optional step d1) is / are manufactured from a non-fossil feedstock.

[0185] 19. Process according to any one of embodiments 13 to 18 wherein at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the CO and / or H2 used for manufacture of the aliphatic C3-C5 aldehyde provided in optional step d1) is formed in step c).

[0186] 20. Process according to any one of embodiments 13 to 19 wherein the carboxylic acid formed in step d2) is selected from the group consisting of propionic acid, n-butanoic acid, n-pentanoic acid, 2-methylpropanoic acid, 2-methylbutanoic acid, 3-methylbutanoic acid, 2,2-dimethylpropanoic acid, 2-ethylhexanoic acid, and 2- propylheptanoic acid.

[0187] 21. Process according to any one of embodiments embodiment 13 to 20 wherein at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the aliphatic C3-C5 aldehydes formed in step c) or the aliphatic alcohols formed in optional step d1) or the aliphatic C9-C13 alcohols formed in step c) which are converted in optional step d2) is / are manufactured from a non-fossil feedstock.

[0188] 22. Process according to any one of embodiments 13 to 21 wherein at least 2.5 wt.-%, more preferably at least 5.0 wt.-% and most preferably at least 7.5 wt.% of the aliphatic C3-C5 aldehydes formed in step c) or the aliphatic alcohols formed in optional step d1) or the aliphatic C9-C13 alcohols formed in step c) which are converted in optional step d2) is / are manufactured from the C2-C4 olefin and / or oligomer thereof formed in steps (i) to (ix) and / or the mixture of CO and H2 formed in steps (i) to (iv).

[0189] 23. Process according to any one of embodiments 1 to 22 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.

[0190] 24. Process according to any one of embodiments 1 to 23 wherein 20 to 70 wt.-%, preferably 20 to 40 wt.-% of said gaseous pyrolysis effluent S2 are separated in step (iv) as high boiling fraction S5 therefrom. 240987W001

[0191] 28

[0192] 25. Process according to any one of embodiments 1 to 24 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.

[0193] 26. Process according to any one of embodiments 1 to 25 wherein said first intermediate stream S4 has a temperature of preferably 200 to 280 °C and more preferably 230 to 270 °C when leaving the at least one quench unit QU.

[0194] 27. Process according to any one of embodiments 1 to 26 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.

[0195] 28. Process according to any one of embodiments 1 to 27 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.

[0196] 29. Process according to any one of embodiments 1 to 28 wherein the high boiling fraction S5 comprises C 11 -C21 + hydrocarbons.

[0197] 30. Process according to any one of embodiments 1 to 29 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.

[0198] 31. Process according to any one of embodiments 1 to 30 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.

[0199] 32. Process according to any one of embodiments 1 to 31 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.

[0200] 33. Process according to any one of embodiments 1 to 32 wherein said second intermediate stream S4' is depleted in C11-C21 + hydrocarbons compared to said first intermediate stream S4. 240987W001

[0201] 29

[0202] 34. Process according to any one of embodiments 1 to 33 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.

[0203] 35. Process according to any one of embodiments 1 to 34 wherein said medium boiling fraction S6 comprises C6-C20 hydrocarbons.

[0204] 36. Process according to any one of embodiments 1 to 35 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.

[0205] 37. Process according to any one of embodiments 1 to 36 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.

[0206] 38. Process according to any one of embodiments 1 to 37 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.

[0207] 39. Process according to any one of embodiments 1 to 38 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.

[0208] 40. Process according to any one of embodiments 1 to 39 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.

[0209] 41. Process according to any one of embodiments 1 to 40 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.

[0210] 42. Process according to any one of embodiments 1 to 41 wherein said low boiling fraction S8 comprises C6-C10 hydrocarbons.

[0211] 43. Process according to any one of embodiments 1 to 42 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. 240987W001

[0212] 30

[0213] 44. Process according to any one of embodiments 1 to 43 wherein a water stream S10 is separated from the third intermediate stream S4" in the second condensation unit CU2.

[0214] 45. Process according to any one of embodiments 1 to 44 wherein said non-condensable stream S7 comprises C1 -C5 hydrocarbons.

[0215] 46. Process according to any one of embodiments 1 to 45 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.

[0216] 47. Process according to embodiment 46 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.

[0217] 48. Process according to embodiment 46 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.

[0218] 49. Process according to embodiment 46 wherein the residence time for the feed stream S1 inside the pyrolysis unit PU2 preferably range from 2.5 to 40 min.

[0219] 50. Process according to any one of embodiments 1 to 49 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 .

[0220] 51. Process according to any one of embodiments 1 to 50 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.

[0221] 52. Process according to any one of embodiments 1 to 51 wherein the at least one quench unit QU and said separation unit SU are combined in a quench and separation unit QSU.

[0222] 53. Process according to any one of embodiments 1 to 52 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. 240987W001

[0223] 31

[0224] 54. Process for manufacturing aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols from C2-C4 olefins and syngas comprising the steps a) providing a C2-C4 olefin or an oligomer thereof, b) providing a mixture of CO and H2, c) contacting the C2-C4 olefin or oligomer thereof provided in step a) and the mixture of CO and H2 provided in step b), preferably in the presence of at least one catalyst, and thereby forming an aliphatic C3-C5 aldehyde or an aliphatic C9-C13 alcohol, characterized in that at least a portion of the C2-C4 olefin provided in step a) and / or at least a portion of the mixture of CO and H2 provided in step b) is manufactured by steps

[0225] (i) providing a feed stream S1 , wherein said feed stream S1 comprises or preferably consists of plastic waste,

[0226] (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,

[0227] (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,

[0228] (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', and converting said stream S5 by a partial oxidation process in at least one gasifier G into a mixture of CO and H2,

[0229] (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",

[0230] (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, 240987W001

[0231] 32

[0232] (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,

[0233] (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, and

[0234] (ix) converting at least one of the streams selected from the group consisting of S6a, S8 and S9 by a steam cracking process in at least one steam cracking unit SCU into C2-C4 olefins and, optionally, converting at least a portion of said C2-C4 olefins into oligomers thereof.

[0235] 55. 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 directly or indirectly fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2, further comprising h) at least one gasifier G, said at least on gasifier G downstream of the separation unit SU and directly or indirectly fluidically connected to the separation unit SU and / or at least one steam cracking unit SCU, said at least one steam cracking unit downstream of and directly or indirectly fluidically connected to at least one of the members selected from the group consisting of at least one first condensation unit CU1, at second condensation unit CU2 and the optional at least one mixing unit MU.

[0236] 56. Pyrolysis plant according to embodiment 55 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. 240987W001

[0237] 33

[0238] 57. Pyrolysis plant according to embodiment 56 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.

[0239] 58. Pyrolysis plant according to any one of embodiments 55 to 57 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.

[0240] 59. Pyrolysis plant according to any one of embodiments 55 to 58 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.

[0241] 60. Pyrolysis plant according to any one of embodiments 55 to 59 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.

[0242] 61. Pyrolysis plant according to any one of embodiments 55 to 60 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.

[0243] 62. Pyrolysis plant according to any one of embodiments 55 to 61 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.

[0244] 63. Use of the pyrolysis plant according to any one of embodiments 55 to 62 for the process according to any one or embodiments 1 to 54.

[0245] The invention will be further explained by the following non-limiting examples.

[0246] Examples

[0247] The 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 S 1 ) 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 240987W001

[0248] 34

[0249] (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 Table 1 .

[0250] T able 1 : parameters used for streams S 1 , S2 and S3 throughout all examples (including comparative examples).

[0251] S1 S2 S3

[0252] T [°C] 25 500 25

[0253] P [bar ( 1.2 1.2 1.2

[0254] Total m 1020 1000 20

[0255] Mole va 0 1 0

[0256] H2[wt- 0.03

[0257] CO [wt.- 0.26

[0258] CO2[wt. 1.22

[0259] H2O [wt. 2.7

[0260] CH4[wt. 0.97

[0261] C2-C5 10.83

[0262] C6-C10 25.92

[0263] C11-C2 38.85

[0264] C21+ [w 17.03

[0265] HA** [wt 2.18 0

[0266] “solids” 100

[0267] Plastic 100 provided

[0268] “mole vapor-frac” corresponds to the molar frac ion of gaseous components in the corresponding stream Sn (0=liquid; 1 =gas)

[0269] ** HA = components comprising at least one hete roatom (O, N, S, halogens), such as nitriles (benzonitrile for example), primary amines (aniline for example), e-caprolactam, chinolines (dimethylchinoline 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.

[0270] Example 1

[0271] The 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.

[0272] 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 240987W001

[0273] 35 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.

[0274] 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.

[0275] 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.

[0276] 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.

[0277] 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.-%. 240987W001

[0278] 36

[0279] Table 2: results from example 1 .

[0280] S4 S5 S6a S6b S7 S8 S9 S10

[0281] T [°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 3

[0282] Total mass flow [kg / h] 2016 208 542 1016 121 106 648 23

[0283] Mole vapor frac 0.957 0 0 0 1 0 0 0

[0284] H2[wt.-%] 0.02 0 0 0 0.27 0 0 0

[0285] CO [wt.-%] 0.13 0 0 0 2.15 0 0 0

[0286] CO2[wt.-%] 0.61 0 0.01 0.01 9.97 0.1 0.02 0.03

[0287] H2O [wt.-%] I .37 0 0.06 0.06 3.38 0.03 0.06 97.4

[0288] CH4[wt-%] 0.48 0 0 0 8.05 0.02 0 0

[0289] C2-C5 [wt-%] 5.7 0.02 0.66 0.66 71.86 17.08 3.34 0.01

[0290] C6-C10 [wt.-%] 28.64 1.38 31.32 31.32 4.15 77.05 38.79 0.01

[0291] C11-C20 [wt-%] 48.27 34.1 57.54 57.54 0.01 5.24 49 0

[0292] C21 + [wt-%] I I .94 63.74 6.92 6.92 0 0 5.79 0

[0293] HA [wt-%] 2.84 0.76 3.49 3.49 0.15 0.48 3 2.55

[0294] D86-0 %1[°C] 191 81 81 - -21 15

[0295] D86-50 % [°C] 366 230 230 - 125 206

[0296] D86-100 %2[°C] 556 386 386 - 206 380

[0297] 1D86-0 % = IBP

[0298] 2D86-100 % = FBP

[0299] Stream 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 a 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 2

[0300] The 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-%. 240987W001

[0301] 37

[0302] Table 3: results from example 2.

[0303] S4 S5 S6a S6b S7 S8 S9 S10

[0304] T [°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 3 Total mass flo 2129.1 270 475 1129 121 111 586 23 [kg / h]

[0305] Mole vapor-fra 0.944 0 0 0 1 0 0 0

[0306] H2[wt.-%] 0.02 0 0 0 0.27 0 0 0

[0307] CO [wt.-%] 0.12 0 0 0 2.14 0 0 0

[0308] CO2[wt.-%] 0.57 0 0.01 0.01 9.94 0.10 0.02 0.03

[0309] H2O [wt.-%] 1.3 0 0.06 0.06 3.56 0.03 0.06 97.4

[0310] CH4[wt.-%] 0.46 0 0 0 8.03 0.02 0 0

[0311] C2-C5 [wt.-% 5.45 0.02 0.69 71.68 17.08 3.34 0.01 C6-C10 [wt.- 30.4 1.89 34.36 34.36 4.22 77.05 38.79 0.01 C11-C20 [wt- 48.41 41.6 56.88 56.88 0.01 5.24 49 0 C21+ [wt-%] 10.28 55.41 4.3 4.3 0 0 5.79 0

[0312] HA [wt.-%] 2.98 1.07 3.7 3.7 0.15 0.48 3 2.55

[0313] D86-0 % [°C] 185 82 - -21 15 D86-50 % [°C 354 216 - 125 194 D86-100 % [° 547 366 - 205 360

[0314] Stream S9 has a final boiling point of 360 °C and, accordingly, is suited as a feedstock for a steam cracking process.

[0315] 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 a 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 3

[0316] The target product is a stream S9 having a final boiling point FBP (determined according to ASTM-D86-23) of

[0317] 340 °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.-%. 240987W001

[0318] 38

[0319] Table 4: results from example 3.

[0320] S4 S5 S6a S6b S7 S8 S9 S10

[0321] T [°C] 239.2 239.2 97 97 25 25 25 25

[0322] P [bar (abs.)] 1.2 1.2 1.2 1.2 1.1 1.1 3 3

[0323] Total mass flo 2302 361 375 1302 122 120 495 23

[0324] Mole vapor-fra 0.925 0 0 0 1 0 0 0

[0325] H2[wt.-%] 0.01 0 0 0 0.27 0 0 0

[0326] CO [wt.-%] 0.11 0 0 0 2.13 0 0 0

[0327] CO2[wt.-%] 0.53 0 0.01 0.01 9.87 0,09 0.03 0.03

[0328] H2O [wt.-%] 1.21 0 0.07 0.07 3.92 0.03 0.06 97.26

[0329] CH4[wt.-%] 0.42 0 0 0 7.97 00.01 0 0

[0330] C2-C5 [wt.-% 5.12 0.03 0.74 0.74 71.3 15.59 4.33 0.01

[0331] C6-C10 [wt.- 33.74 3.01 39.75 39.75 4.36 78.45 49.1 0.01

[0332] C11-C20 [wt- 47.16 50.23 53.55 53.55 0.01 5.32 41.89 0

[0333] C21 + [wt-%] 8.56 45.07 2.05 2.05 0 0 1.56 0

[0334] HA [wt.-%] 3.12 1.66 3.84 3.84 0.16 0.5 3.03 2.7

[0335] D86-0 % [°C] 172 79 79 - -20 14

[0336] D86-50 % [°C 335 205 205 - 126 172

[0337] D86-100 % [° 540 345 345 - 201 340

[0338] Stream 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 4

[0339] The 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.-%. 240987W001

[0340] 39

[0341] Table 5: results from example 4.

[0342] S4 S5 S6a S6b S7 S8 S9 S10

[0343] T [°C] 189.7 189.7 - 97 25 25 25 25

[0344] P [bar (abs.)] 1.2 1.2 - 1.2 1.1 1.1 3 3

[0345] Total mass flo 3003 678 0 2003 163 159 159 1

[0346] Mole vapor-fra 0.868 0 0 0 1 0 0 0

[0347] H2[wt.-%] 0.01 0 - 0 0.2 0 0 0

[0348] CO [wt.-%] 0.09 0 - 0 1.6 0 0 0

[0349] CO2[wt.-%] 0.41 0 - 0.01 7.44 0.03 0.03 0.01

[0350] H2O [wt.-%] 0.94 0.01 - 0.07 16.24 0.03 0.34 95.19

[0351] CH4[wt.-%] 0.33 0 - 0 5.98 0 0 0

[0352] C2-C5 [wt-% 4.2 0.05 - 0.89 59.67 6,88 6.86 0

[0353] C6-C10 [wt.- 55.32 15.43 - 70 8.62 88.44 88.15 0.01

[0354] C11-C20 [wt- 30.92 56.43 - 26.96 0.04 3.77 3.76 0

[0355] C21+ [wt-%] 5.78 25.12 - 0.16 0 0 0 0

[0356] HA [wt-%] 2 2.96 - 1.91 0.21 0.84 0.86 4.79

[0357] D86-0 % [°C] 143 - 71 - 3 3

[0358] D86-50 % [°C 275 - 153 - 132 132

[0359] D86-100 % [° 510 - 279 - 196 196

[0360] Stream 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 1

[0361] The 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 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-%. 240987W001

[0362] 40

[0363] Table 6: results from comparative example 1 .

[0364] S6' S7 S8 S9 S10

[0365] T [°C] 97 25 25 25 25 p [bar (abs.)] 1.2 1.1 1.1 3 3

[0366] Total mass flow [kg / h] 761 120 96 857 23

[0367] Mole vapor-frac 0 1 0 0 0

[0368] H2[wt.-%] 0 0.27 0 0 0

[0369] CO [wt.-%] 0 2.16 0 0 0

[0370] CO2[wt-%] 0 10.03 0.11 0.02 0.03

[0371] H2O [wt-%] 0.06 3.05 0.03 0.06 97.58

[0372] CH4[wt.-%] 0 8.1 0.02 0 0

[0373] C2-C5 [wt-%] 0.55 72.23 18.39 2.54 0.01

[0374] C6-C10 [wt.-%] 23.87 3.99 76.08 29.7 0.01

[0375] C11-C20 [wt-%] 50.43 0.01 4.92 45.35 0

[0376] C21 + [wt-%] 22.38 0 0.01 19.88 0

[0377] HA [wt-%] 2.71 0.15 0.46 2.46 2.38

[0378] D86-0 % [°C] 86 - -22 19

[0379] D86-50 % [°C] 251 - 123 235

[0380] D86-100 % [°C] 503 - 203 490

[0381] No 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.

[0382] Comparative Example 2

[0383] The process applied in comparative example 2 is shown in Figure 3 and based on the teachings of

[0384] CN 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').

[0385] 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-%. 240987W001

[0386] 41

[0387] Table 7: results from comparative example 2.

[0388] S4 S5 S6a S6b S7 S8 S9 S10

[0389] T [°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 3

[0390] Total mass flow [kg / h] 2000 0 761 1000 120 96 857 23

[0391] Molar vapor-frac 0.926 0 0 0 1 0 0 0

[0392] H2[wt.-%] 0.02 0 0 0 0.27 0 0 0

[0393] CO [wt.-%] 0.13 0 0 0 2.16 0 0 0

[0394] CO2[wt.-%] 0.61 0 0 0 10.03 0.11 0.02 0.03

[0395] H2O [wt.-%] 1.38 0 0.06 0.06 3.05 0.03 0.06 97.58

[0396] CH4[wt.-%] 0.49 0 0 8.10 0.02 0 0

[0397] C2-C5 [wt.-%] 5.69 0 0.55 0.55 72.23 18.39 2.54 0.01

[0398] C6-C10 [wt.-%] 24.89 0 23.87 23.87 3.99 76.08 29.70 0.01

[0399] C11-C20 [wt-%] 44.64 0 50.43 50.43 0.01 4.92 45.35 0

[0400] C21+ [wt-%] 19.70 0 22.38 22.38 0 0.01 19.88 0

[0401] HA [wt.-%] 2.44 0 2.71 2.71 0.15 0.46 2.46 2.38

[0402] D86-0 % [°C] 86 86 - -22 19

[0403] D86-50 % [°C] 251 251 - 123 235

[0404] D86-100 % [°C] 503 503 - 203 490

[0405] No high boiling fraction S5 was separated from the gaseous pyrolysis effluent S2. The resulting pyrolysis oil stream

[0406] 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.

Claims

1. 240987W00142Claims1 . Process for manufacturing aliphatic C3-C5 aldehydes and aliphatic C9-C13 alcohols from C2-C4 olefins and syngas comprising the steps a) providing a C2-C4 olefin or an oligomer thereof, b) providing a mixture of CO and H2, c) contacting the C2-C4 olefin or oligomer thereof provided in step a) and the mixture of CO and H2 provided in step b), preferably in the presence of at least one catalyst, and thereby forming an aliphatic C3-C5 aldehyde or an aliphatic C9-C13 alcohol, wherein the process, prior to step a), also comprises the steps of(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', and converting said stream S5 by a partial oxidation process in at least one gasifier G into a mixture of CO and H2,(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 second240987W00143 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,(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 and(ix) converting at least one of the streams selected from the group consisting of S6a, S8 and S9 by a steam cracking process in at least one steam cracking unit SCU into C2-C4 olefins and, optionally, converting at least a portion of said C2-C4 olefins into oligomers thereof.

2. Process according to claim 1 wherein the C2-C4 olefin provided in step a) is selected from the group consisting of ethylene, propylene, 1 -butene, trans-2-butene and cis-2-butene or wherein the oligomer of C2-C4 olefin provided in step a) is selected from the group consisting of 2,4,4-trimethyl-1 -pentene, 2,4,4- trimethyl-2-pentene and dodec-1-ene.

3. Process according to claim 1 or 2 wherein the mixture of CO and H2 provided in step b) has a molar ratio CO :H2 of 30 : 70 to 50 : 50, most preferably of 35 : 65 to 45 : 55.

4. Process according to any one of claims 1 to 3 wherein the aliphatic C3-C5 aldehyde formed in step c) is selected from the group consisting of propanal, 1 -butanal, 2-butanal, 1-pentanal, and 2-methylbutanal or wherein the aliphatic C9-C13 alcohol formed in step c) is selected from the group consisting of 3,5,5- trimethylhexane-1-ol, dimethyl-1 -heptanole, methyl-1-octanolen, 1 -tridecanole, 2-tridecanole, 3-tridecanole, 4- tridecanole, 5-tridecanole, 6-tridecanole, 7-tridecanole and isomeric mixtures of tridecanole.

5. Process according to any one of claims 1 to 4 wherein preferably at least 2.5 wt.-%, more preferably at least 5.0 wt.-%, most preferably 7.5 wt.-% of the C2-C4 olefin or the oligomer thereof provided in step a) is manufactured by steps (i) to (ix).

6. Process according to any one of claims 1 to 5 wherein the at least one catalyst in step c) is preferably a homogeneous catalyst, more preferably a homogeneous catalyst comprising at least one metal selected from the group consisting of cobalt, rhodium, iridium, palladium, platinum, and ruthenium and most preferably a homogeneous catalyst comprising at least one metal selected from the group consisting of cobalt and rhodium.

7. Process according to any of claims 1 to 6 comprising the further step d1) converting the aliphatic C3-C5 aldehyde formed in step c) into an aliphatic C3-C5 alcohol or two different aliphatic C3-C5 aldehydes of which at least one was formed in step c) into an aliphatic alcohol and / or240987W00144 d2) converting the aliphatic C3-C5 aldehyde formed in step c) or the aliphatic alcohol formed in optional step d1) or the aliphatic C9-C13 alcohols formed in step c) into a carboxylic acid.

8. Process according to claim 7 wherein the aliphatic C3-C5 alcohol formed in step d1) is selected from the group consisting of 1 -propanol, 2-propanol, 1 -butanol, 2-methylpropanol, 1 -pentanol, 2-methylbutanol, and 3- methylbutanol and wherein the aliphatic alcohol formed in step d1) from two different aliphatic C3-C5 aldehydes of which at least one was formed in step c) is selected from the group consisting of 2- propylheptanol and 2-ethylhexanol and / or wherein the carboxylic acid formed in step d2) is selected from the group consisting of propionic acid, n-butanoic acid, n-pentanoic acid, 2-methylpropanoic acid, 2- methylbutanoic acid, 3-methylbutanoic acid, 2,2-dimethylpropanoic acid, 2-ethylhexanoic acid, and 2- propylheptanoic acid.

9. Process according to any one of claims 1 to 8 wherein 20 to 70 wt.-%, preferably 20 to 40 wt.-% of said gaseous pyrolysis effluent S2 are separated in step (iv) as high boiling fraction S5 therefrom.

10. Process according to any one of claims 1 to 9 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.

11. Process according to any one of claims 1 to 10 wherein said first intermediate stream S4 has a temperature of preferably 200 to 280 °C and more preferably 230 to 270 °C when leaving the at least one quench unit QU.

12. Process according to any one of claims 1 to 11 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.

13. Process according to any one of claims 1 to 12 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.

14. Process according to any one of claims 1 to 13 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.

15. 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,240987W00145 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 directly or indirectly fluidically connected to the at least one splitting unit SPU and said at least one second condensation unit CU2, further comprising h) at least one gasifier G, said at least on gasifier G downstream of the separation unit SU and directly or indirectly fluidically connected to the separation unit SU and / or at least one steam cracking unit SOU, said at least one steam cracking unit downstream of and directly or indirectly fluidically connected to at least one of the members selected from the group consisting of at least one first condensation unit CU1, at second condensation unit CU2 and the optional at least one mixing unit MU.

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