Process for purifying a pyrolysis oil

Abstract

The present invention relates to a process for purifying a pyrolysis oil comprising an extraction step prior to a thermal treatment step, a production unit for carrying out said process and a purified pyrolysis oil obtained or obtainable by said process.

Description

[0001] Process for purifying a pyrolysis oil

[0002] The present invention relates to a process for purifying a pyrolysis oil comprising an extraction step prior to a thermal treatment step, a production unit for carrying out said process and a purified pyrolysis oil obtained or obtainable by said process.

[0003] Currently, plastic waste is still largely landfilled or incinerated for heat generation. Chemical recycling is an attractive way to convert waste plastic material into useful chemicals. An important technique for chemically recycling plastic waste is pyrolysis. The pyrolysis is a thermal degradation of plastic waste in an inert atmosphere and yields value added products such as pyrolysis gas, liquid pyrolysis oil and char (residue), wherein pyrolysis oil is the major product. The pyrolysis gas and char can be used as fuel for generating heat, e.g. for reactor heating purposes. The pyrolysis oil can be used as source for syngas production and / or processed into chemical feedstock such as ethylene, propylene, C4 cuts, etc. for example in a (steam) cracker.

[0004] Typically, the plastic waste is mixed plastic waste composed of different types of polymers. The polymers are often composed of carbon and hydrogen in combination with other elements such as chlorine, bromine, fluorine, sulfur, oxygen and nitrogen that complicate recycling efforts. The elements other than carbon and hydrogen may be harmful during the further processing of the crude pyrolysis oil, since they may deactivate or poison catalysts used in the further processing of the pyrolysis oil. During (steam) cracking, halogen-containing compounds as well as acids and oxygen-containing compounds can damage the cracker by corrosion e.g. in that they release hydrogen halide. Sulfur-containing compounds can deactivate or poison catalysts used in the cracker, or can contaminate the cracker products. Nitrogen containing impurities may also poison downstream catalysts. In addition, they may cause a safety problem by forming explosive NOx when heated. When mixed plastics containing polyvinyl chloride (PVC) is thermally degraded, compounds having double carbon bonds and hydrogen chloride is formed. The hydrogen chloride liberated from PVC attacks the compounds having carbon-carbon double bonds leading to the formation of chlorinated organic compounds. Plastic waste typically contains heteroatom containing additives such as stabilizers and plasticizers that have been incorporated to improve the performance of the polymers. Such additives also often comprise nitrogen, halogen and sulfur containing compounds and heavy metals. For example, waste engine oils, transformer oils, hydraulic oils and machine oils may contain heavy metal abrasion. The heavy metals are often toxic and the quality of the pyrolysis oil is reduced by the presence of heavy metal impurities. Furthermore, plastic waste often may be uncleaned plastics with residue that may also contain elements other carbon and hydrogen. Therefore, a high quality pyrolysis oil rich in carbon and hydrogen and low in elements other than carbon and hydrogen is preferred as feedstock to prevent catalyst deactivation and corrosion problems in downstream refinery processes.

[0005] WO 2017 / 083018 A1 discloses a process for reducing chloride content of a hydrocarbon feed stream. WO 2014 / 165859 A1 discloses a process for purifying a pyrolysis oil comprising one or two extraction steps. Further, WO 2020 / 178597 A1 discloses a process for upgrading a pyrolysis oil comprising treating the pyrolysis oil with an aqueous solution, preferably consisting of water, and an alkane and treating the obtained organic phase with an upgrading solution comprising polar organic solvent.

[0006] However, there is still a need to provide improved process for purifying pyrolysis oil obtained from plastic waste. In particular, there is still a need to provide improved process which exhibits longer time on stream, lower pressure drop, and avoid fouling. This was not solved with the processes of the prior art.

[0007] Therefore, there is a need to provide a process for purifying pyrolysis oils, preferably obtained from waste material, in particular by reducing the total acid number as well as chlorine, oxygen, nitrogen contents. Indeed, there is a need to provide high value purified pyrolysis oils while using an economic process.

[0008] It was surprisingly found that the process of the present invention permits to reduce the total acid number as well as chlorine, oxygen, and nitrogen contents, such reduced amounts being particularly adapted for subsequent storage and / or steam cracking. Further, it was surprisingly found that the process of the present invention was an economic process providing high value purified pyrolysis oils.

[0009] Therefore, the present invention relates to a process for purifying a pyrolysis oil, the process comprising:

[0010] (i) providing a stream F0 comprising a pyrolysis oil, the pyrolysis oil comprising one or more halogenated organic compounds and one or more organic compounds comprising conjugated double bonds;

[0011] (ii) subjecting the stream F0 provided in (i) to extraction in at least one extraction zone ZE, obtaining a stream F1 comprising the extracted pyrolysis oil, wherein (ii) comprises:

[0012] (ii.1 ) introducing F0 into ZE;

[0013] (ii .2) bringing in contact F0 with water and a base B into ZE at a temperature in the range of from 10 to 200 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 ;

[0014] (ii.3) separating PA from Po, obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil;

[0015] (iii) subjecting the stream F1 obtained according to (ii) to thermal treatment in at least one thermal treating zone ZP, ZP being located downstream of ZE, obtaining a stream F2 being depleted, compared to F1 , in one or more of the one or more organic compounds comprising conjugated double bonds and the one or more halogenated organic compounds.

[0016] Preferably, the thermal treatment according to (iii) is performed at a temperature in the range of from 80 to 400 °C.

[0017] Generally, from 1 to 100 weight-% or from 5 to 100 weight-% or from 10 to 100 weight-% or from 20 to 100 weight-% or from 30 to 100 weight-% or from 40 to 100 weight-% or from 50 to 100 weight-% or from 60 to 100 weight-% or from 70 to 100 weight-% or from 80 to 100 weight- % or from 90 to 100 weight-% of F0 may consist of pyrolysis oil.

[0018] Preferably, from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, of F0 consist of pyrolysis oil.

[0019] It is possible that from 99.5 to 100 weight-% or from 99.8 to 100 weight-% or from 99.9 weight- % of F0 consist of pyrolysis oil.

[0020] The pyrolysis oil according to (i), the oil to be purified, can have any total acid number (TAN). Preferably, the pyrolysis oil according to (i) has a total acid number (TAN) in the range of from 0.5 to 60 mg KOH / g(F0), more preferably in the range of from 1 to 40 mg KOH / g(F0), more preferably in the range of from 3 to 20 mg KOH / g(FO)determined as described in Reference Example 1.

[0021] The pyrolysis oil according to (i), the oil to be purified, can have any oxygen content. Preferably, the pyrolysis oil according to (i) has an oxygen content in the range of from 0.1 to 15 g(G) / 100g(F0), more preferably in the range of from 0.5 to 10 g(G) / 100g(F0), more preferably in the range of from 0.1 to 5 g(G) / 100g(F0) determined as described in Reference Example 5.

[0022] Preferably, the one or more halogenated organic compounds comprised in the pyrolysis oil according to (i) comprise one or more of mono- oligo- or polyhalogenated aromatic compounds, alkylhalides and alkenylhalides. The pyrolysis oil according to (i), the oil to be purified, can have any total chlorine content. Preferably, the pyrolysis oil according to (i) has a total chlorine content in the range of from 30 to 3,000 wppm (ppm by weight), more preferably from 30 to 500 wppm, more preferably from 30 to 100 wppm, determined as described in Reference Example 3.1.

[0023] The pyrolysis oil according to (i), the oil to be purified, can have any nitrogen content. Preferably, the pyrolysis oil according to (i) has a nitrogen content in the range of from 10 to 20,000 wppm (ppm by weight), more preferably from 50 to 5,000 wppm, more preferably from 100 to 4,000 wppm, determined as described in Reference Example 2.

[0024] The pyrolysis oil according to (i), the oil to be purified, can have any sulfur content. Preferably, the pyrolysis oil according to (i) has a sulfur content in the range of from 10 to 30,000 ppm by weight (wppm), more preferably from 20 to 5,000 wppm, more preferably from 50 to 3,000 wppm, determined as described in Reference Example 6.

[0025] The pyrolysis oil according to (i), the oil to be purified, can have any amount of one or more organic compounds comprising conjugated double bonds. Preferably, the pyrolysis oil according to (i) comprises the one or more organic compounds comprising conjugated double bonds in a total amount in the range of from 0.1 to 75 g(l2) / 100 g, more preferably from 0.4 to 60 g(l2) / 100 g, more preferably from 1 to 30 g(l2) / 100 g of the pyrolysis oil, determined as described in Reference Example 4.

[0026] The pyrolysis oil according to (i), the oil to be purified, can have any styrene content. Preferably, Preferably the pyrolysis oil according to (i) has a styrene content in the range of from 0.2 to 30 Area%, more preferably in the range of from 1 to 20 Area%, determined as described in Reference Example 7.

[0027] Preferably, the one or more organic compounds comprising conjugated double bonds comprise one or more organic compounds according to formula (I)

[0028] R1R2C1=C2R3-C3R4=X (I) wherein =X is =0, =S, =NR5, or =C4R6R7, preferably =C4R6R7; more preferably wherein R1, R2, R3, R4, R5are, independently of each other, H, alkyl having from 1 to 6 carbon atoms, alkenyl having from 1 to 6 carbon atoms, or aryl having from 5 to 10 carbon atoms, more preferably H; more preferably wherein R6and R7are, independently of each other, H, alkyl having from 1 to 6 carbon atoms, alkenyl having from 1 to 6 carbon atoms, or aryl having from 5 to 10 carbon atoms, more preferably H; or more preferably wherein either R4and R6or R4and R7are linked together, thus forming, together with C3=C4, an aromatic ring more preferably having 5 or 6 members.

[0029] Preferably, the one or more organic compounds comprising conjugated double bonds comprise one or more of butadiene, isoprene, dienes having 5 or 6 carbon atoms, styrene, methylstyrene, indene, substituted styrene, substituted indene, and 3-methyl-2-butenal, more preferably comprise one or more of butadiene, isoprene, dienes having 5 or 6 carbon atoms, styrene, methylstyrene, indene, and 3-methyl-2-butenal.

[0030] Preferably, the one or more organic compounds comprising conjugated double bonds comprise styrene.

[0031] Preferably, the pyrolysis oil comprised in F0 is obtained from a waste material.

[0032] In the context of the present invention, the pyrolysis oil comprised in F0 is preferably obtained from pyrolyzing a waste material, the waste material being one or more of plastics and tires.

[0033] Preferably, the stream F0 is a liquid stream.

[0034] In the context of the present invention, for example, for maintaining F0 in the liquid state, one can heat the pyrolysis oil as known by the skilled person.

[0035] Step (ii)

[0036] Preferably, no organic solvent is used in the extraction according to (ii).

[0037] Preferably, there is no washing with a hydrocarbon stream, such as alkane, in (ii), or between (ii) and (iii).

[0038] Preferably, the extraction according to (ii) is performed at a pressure PE in the range of from 0.8 to 1.2 bar(abs), more preferably in the range of from 0.9 to 1.1 bar(abs).

[0039] Alternatively, the extraction according to (ii) is performed at a pressure ps in the range of from 0.5 to 5 bar(abs), more preferably in the range of from 0.7 to 3 bar(abs), more preferably in the range of from 0.9 to 2 bar(abs). Preferably, the extraction according to (ii) is performed at a temperature in the range of from 10 to 95 °C, more preferably in the range of from 15 to 90°C, more preferably in the range of from 20 to 85 °C, more preferably in the range of from 25 to 80 °C.

[0040] Preferably, when the temperature of the extraction (ii) is < 95 °C, the extraction according to (ii) is performed at a pressure in the range of from 0.8 to 1 .2 bar(abs), more preferably in the range of from 0.9 to 1.1 bar(abs), more preferably at about 1 bar(abs).

[0041] In the context of the present invention, alternatively, when the temperature of the extraction (ii) > 95 °C, the pressure is preferably in the range of from 1 to 16 bar(abs).

[0042] In the context of the present invention, it is noted that the pH of the aqueous phase of a mixture of water and the pyrolysis oil provided in (i) is preferably in the range of from 0 to 6, more preferably in the range of from 1 to 5.5.

[0043] Preferably, the base B is one or more of an alkali metal compound, an alkaline earth metal compound, such as alkaline earth metal oxide and / or hydroxide (e.g. calcium hydroxide), and ammonia. More preferably B is an alkali metal compound being one or more of potassium hydroxide, sodium hydroxide, potassium carbonate, sodium carbonate, potassium bicarbonate and sodium bicarbonate, more preferably one or more of potassium hydroxide, sodium hydroxide, potassium carbonate and sodium carbonate, more preferably one or more of potassium hydroxide and sodium hydroxide, more preferably potassium hydroxide or sodium hydroxide, more preferably potassium hydroxide.

[0044] Preferably, water used in (ii) is demineralized water.

[0045] Preferably, for the extraction according to (ii), the weight ratio of water to F0 in ZE is in the range of from 0.05:1 to 2:1 , more preferably in the range of from 0.1 :1 to 1.5:1 , more preferably in the range of from 0.1 :1 to 1.2:1 , more preferably in the range of from 0.1 :1 to 0.7:1 , more preferably in the range of from 0.2:1 to 0.5:1 , more preferably in the range of from 0.3:1 to 0.5:1.

[0046] In the context of the present invention, the amount of the base B which is used in (ii) is preferably determined for obtaining a pH of the aqueous phase PA of M be in the range of from 7 to 11 , more preferably from 7 to 10. Alternatively, the amount of the base B which us used in (ii) is preferably determined for obtaining a pH of the aqueous phase PA of M be in the range of from 7.5 to 11. This can be realized by the skilled person based on its general knowledge. Preferably, the pH of the aqueous phase PA of M obtained according to (ii.2) is in the range of from 7 to 10.

[0047] Alternatively, the pH of the aqueous phase PA of M obtained according to (ii.2) is in the range of from 7.5 to 11.

[0048] Preferably, the pH of the aqueous phase PA of M obtained according to (ii.2) is measured by one or more pH-sensor located in ZE.

[0049] As to (ii.2), according to an alternative, preferably (ii.2) comprises

[0050] (11.2.1 ) introducing water and B, preferably a mixture of water and B, into ZE;

[0051] (11.2.2) bringing in contact, more preferably mixing, F0 with water and B, more preferably the mixture of water and B, into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7 to 10.

[0052] As to (ii.2), according to a further alternative, preferably (ii.2) comprises

[0053] (ii.2.1 ’) introducing water into ZE;

[0054] (ii.2.2’) bringing in contact, more preferably mixing, F0 with water into ZE, obtaining a mixture comprising water and the pyrolysis oil;

[0055] (ii.2.3’) introducing B into ZE and bringing in contact, more preferably mixing, B with the mixture obtained in (ii.2.2’) into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7 to 10.

[0056] As to (ii.2), according to a second alternative, preferably (ii.2) comprises

[0057] (11.2.1 ) introducing water and B, preferably a mixture of water and B, into ZE;

[0058] (11.2.2) bringing in contact, more preferably mixing, F0 with water and B, more preferably the mixture of water and B, into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11.

[0059] As to (ii.2), according to a third alternative, preferably (ii.2) comprises

[0060] (ii.2.1 ’) introducing water into ZE;

[0061] (ii.2.2’) bringing in contact, more preferably mixing, F0 with water into ZE, obtaining a mixture comprising water and the pyrolysis oil;

[0062] (ii.2.3’) introducing B into ZE and bringing in contact, more preferably mixing, B with the mixture obtained in (ii.2.2’) into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11.

[0063] Preferably, (ii.2) comprises

[0064] (ii.2.1 ’) introducing water into ZE;

[0065] (ii.2.2’) bringing in contact, more preferably mixing, F0 with water into ZE, obtaining a mixture M1 comprising water and the pyrolysis oil, wherein the pH of the aqueous phase of M1 has a pH, more preferably measured by a pH-sensor in ZE;

[0066] (ii.2.3’) adjusting the pH of the aqueous phase of M1 by introducing B into ZE and bringing in contact, more preferably mixing, B with M1 obtained in (ii.2.2’) into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, wherein the pH of the aqueous phase PA of M is in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 , and pH of the aqueous phase PA of M > pH of the aqueous phase of M1.

[0067] Preferably, separating PA from Po according to (ii.3) is performed by decantation, or centrifugation, preferably decantation.

[0068] Preferably, (ii) comprises

[0069] (11.1) introducing F0 into a mixing unit UM1 comprised in ZE;

[0070] (11.2) mixing F0 with water and a base B into UM1 at a temperature in the range of from 10 to 200 °C, more preferably from 10 to 95 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 ; removing M from UM1;

[0071] (11.3) separating PA from Po, wherein (ii.3) comprises

[0072] (ii.3.1 ) passing M into a liquid-liquid separation unit US1 comprised in ZE, US1 being located downstream of UM1 , obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil; removing F1 from ZE.

[0073] Preferably, the extraction unit UM1 is one or more of a stirred vessel, a mixing pump and a static mixer, more preferably a stirred vessel.

[0074] Preferably, the liquid-liquid separation unit US1 is one or more of a hydrocyclone, a settler tank and a centrifuge, more preferably a decanter, a hydrocyclone, a settler tank or a centrifuge, more preferably a settler tank. Preferably, UM1 and US1 are distinct units. It is also conceivable that UM1 and US1 are / form a mixer-settler.

[0075] Alternatively, preferably, (ii) comprises

[0076] (11.1) introducing F0 into a mixing unit UM1 comprised in ZE;

[0077] (11.2) mixing F0 with water and a base B into UM1 at a temperature in the range of from 10 to 200 °C, preferably from 10 to 95 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 ; removing M from UM1;

[0078] (11.3) separating PA from Po, wherein (ii.3) comprises

[0079] (ii.3.1 ’) passing M into a liquid-liquid separation unit US1 comprised in ZE, US1 being downstream of UM1 , obtaining a stream FA comprising PA and a stream F1” comprising Po being the extracted pyrolysis oil; removing F1” from US1;

[0080] (ii.3.2’) subjecting the stream F1” provided in (ii.3.1 ’) to washing, obtaining a stream

[0081] F1 comprising the extracted pyrolysis oil which has been purified, wherein (iii.3.2’) comprises:

[0082] (A) introducing F1” into a mixing unit UM2 comprised in ZE, UM2 being located downstream of US1 in ZE; mixing F1” with water in UM2 at a temperature T2 in the range of from 10 to 95 °C, obtaining a mixture comprising an aqueous phase PA(2) and an organic phase Po(2), the pH of the aqueous phase PA(2) of M2 being in the range of from 7.5 to 11, pH of PA(2) < pH of PA; passing the obtained mixture into a liquid-liquid separation unit US2 comprised in ZE, US2 being located downstream of UM2, obtaining a stream F1 comprising the extracted pyrolysis oil which has been purified Po(2); or

[0083] (B)

[0084] - introducing F1” into an extraction column UM+IIS comprised in ZE;

[0085] - introducing water into UM+IIS;

[0086] - bringing in contact F1” with water in UM+IIS at a temperature T2’ in the range of from 10 to 95 °C, obtaining a stream FA(2) comprising an aqueous phase PA(2), the pH of the aqueous phase PA(2) of M2 being in the range of from 7.5 to 11 , pH of PA(2) < pH of PA, and obtaining a stream F1 comprising the extracted pyrolysis oil which has been purified Po(2).

[0087] In the context of the present invention, preferably, the weight ratio of water to F1” is in the range of from 0.05:1 to 2:1 , more preferably in the range of from 0.1 :1 to 1.5:1 , more preferably in the range of from 0.1 :1 to 1.2:1 , more preferably in the range of from 0.1 :1 to 0.7:1.

[0088] Preferably, T2 according to (A) or T2’ according to (B) is in the range of from 15 to 85 °C, more preferably in the range of from 20 to 80 °C.

[0089] Preferably, the at least one extraction zone ZE comprises one or more mixing units and one or more liquid-liquid separation units. More preferably, according to (A), the at least one extraction zone ZE comprises a mixing unit UM1 , a mixing unit UM2, a liquid-liquid separation unit US1 and a liquid-liquid separation unit US1 , more preferably UM1 is located upstream of US1 , US1 is located downstream of UM1 and upstream of UM2, UM2 is located upstream of US2 and downstream of US1 and US2 is located downstream of UM2.

[0090] Preferably, the extraction unit UM1 is one or more of a stirred vessel, a mixing pump and a static mixer, more preferably a stirred vessel.

[0091] Preferably, the liquid-liquid separation unit US1 is one or more of a hydrocyclone, a settler tank and a centrifuge, more preferably a decanter, a hydrocyclone, a settler tank or a centrifuge, more preferably a settler tank.

[0092] Preferably, the extraction unit UM2 is one or more of a stirred vessel, a mixing pump and a static mixer, more preferably a stirred vessel.

[0093] Preferably, the liquid-liquid separation unit US2 is one or more of a hydrocyclone, a settler tank and a centrifuge, more preferably a decanter, a hydrocyclone, a settler tank or a centrifuge, more preferably a settler tank.

[0094] In the context of the present invention, UM2 and US2 are distinct units.

[0095] Alternatively, more preferably, according to (B), the at least one extraction zone ZE comprises a first mixing unit UM1 , a liquid-liquid separation unit US1 and an extraction column UM+IIS, more preferably UM1 is located upstream of US1 , US1 is located downstream of UM1 , UM+IIS is located downstream of UM+IIS.

[0096] In the context of the present invention, optionally, the at least one extraction zone ZE further comprises one or more filtration units, the filtration units being preferably filters. Using a filter means often a discontinuous solid-liquid-separation, where the pressure difference is increasing with increasing filtration time. After a certain amount of pressure difference or filtration time, the solids have to be removed from the filter via a backflush by a fluid or gas or a mixture of both (e.g. disposal filter, backflush filter) or by an automatic system (e.g. automatic cleaning filter) or rotating or vibrating (e.g. pressure leaf filter, candle filter, filter press). During the removal of the solids, a second parallel filter is started operation until a certain pressure difference or filtration time is reached, where the solid emptied filter will be in operation again.

[0097] The filtration can be performed with disposal filter (e.g. bag filter, filter with filter sheets or membranes), where the solids are removed by back flushing or the solids remain on the filter cloth, which lead to a substitution of the filter after a certain pressure difference or operational time. The filtration can be supported by the use of a filter aid to improve the filtration behavior. That can lead to a potential usage of a continuous filter (e.g. belt filter, drum filter).

[0098] Centrifuges can be used for a discontinuous solid-liquid-separation or continuous solid-liquid- separation depending on the centrifuge type. Centrifuges (e.g. decanter centrifuge, separator centrifuge) can be used in a 2 phase (solid-liquid) or 3 phase-system of two liquid phases and solids to separate the solids from the liquid or liquids and the liquid from the liquid. In a separator centrifuge the solids have to be released after the centrifuge loaded to a maximum of solids (discontinuous) compared to a decanter centrifuge, where the solids are continuously separated and removed. The centrifugation can be supported by the use of flocculants to improve the centrifugation behavior.

[0099] Preferably, (ii) consists of (ii.1 ), (ii.2) and (ii.3).

[0100] Preferably, (ii.3) consists of (ii.3.1 ) or consists of (ii.3.1 ’) and (ii.3.2’).

[0101] Preferably, the stream F1 comprising the extracted pyrolysis oil obtained according to (ii) prior to be subjected to (iii) or (iv) has a total acid number (TAN) which is lower than the TAN of the pyrolysis oil provided in (i), more preferably said extracted pyrolysis oil has a TAN in the range of from 0 to 20 mg KOH / g(F1), more preferably in the range of from 0 to 4.5 mg KOH / g(F1) , determined as described in Reference Example 1. Preferably, the stream F1 comprising the extracted pyrolysis oil obtained according to (ii) prior to be subjected to (iii) or (iv) has an oxygen content equal to or lower than, more preferably lower than, the oxygen content of the pyrolysis oil provided in (i). More preferably, the extracted pyrolysis oil obtained according to (ii) prior to be subjected to (iii) or (iv) has an oxygen content in the range of from 0 to 2 g(0) / 100g(F1), determined as described in Reference Example 5.

[0102] Preferably, the stream F1 comprising the extracted pyrolysis oil obtained according to (ii) prior to be subjected to (iii) or (iv) has a nitrogen content equal to or lower than, more preferably lower than, the nitrogen content of the pyrolysis oil provided in (i). More preferably, the extracted pyrolysis oil obtained according to (ii) prior to be subjected to (iii) or (iv) has a nitrogen content in the range of from 10 to 20,000 wppm (ppm by weight), more preferably from 50 to 5,000 wppm, more preferably from 100 to 4000 wppm , determined as described in Reference Example 2.

[0103] Preferably, from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of F1 consist of pyrolysis oil.

[0104] Step (iii)

[0105] Preferably, the thermal treatment according to (iii) is one or more of dehalogenation, hydrogenation, hydroprocessing, heat-up for dehalogenation, heat-up for hydrogenation, heat-up for hydroprocessing and distillation.

[0106] - Dehalogenation & Hydrogenation

[0107] Preferably, (iii) comprises

[0108] (111.1) optionally subjecting the stream F1 obtained according to (ii) to hydrogenation in at least one reaction zone ZH containing a heterogeneous hydrogenation catalyst, ZH being comprised in ZP, obtaining a stream FH being depleted, compared to F1 , in the one or more organic compounds comprising conjugated double bonds;

[0109] (111.2) subjecting the stream F1 obtained according to (ii), or FH obtained according to (iii.1 ), to dehalogenation in at least one dehalogenation zone ZD comprised in ZP, and located downstream of ZH if present, obtaining a stream F2 being depleted, compared to F1 , or FH when (iii.1) is performed, in the one or more halogenated organic compounds.

[0110] Dehalogenation The term “dehalogenation” as used in the context of the present invention generally comprises “dechlorination”, “debromination” as well as “defluorination”. According to the present invention, the term “dehalogenation” preferably comprises “dechlorination”. If, e.g., the pyrolysis oil to be subjected to the process according to the present invention does not contain brominated organic compounds and fluorinated organic compounds, but only chlorinated compounds as halogenated organic compounds, the term “dehalogenation” would be directed to “dechlorination”, and the process of the invention would be a process for purifying a pyrolysis oil, the process comprising

[0111] (i) providing a stream F0 comprising a pyrolysis oil, the pyrolysis oil comprising one or more chlorinated organic compounds and one or more organic compounds comprising conjugated double bonds;

[0112] (ii) subjecting the stream F0 provided in (i) to extraction in at least one extraction zone ZE, obtaining a stream F1 comprising the extracted pyrolysis oil, wherein (ii) comprises:

[0113] (ii.1 ) introducing F0 into ZE;

[0114] (11.2) bringing in contact F0 with water and a base B into ZE at a temperature in the range of from 10 to 200 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 ;

[0115] (11.3) separating PA from Po, obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil;

[0116] (iii) subjecting the stream F1 obtained according to (ii) to thermal treatment in at least one thermal treating zone ZP, ZP being located downstream of ZE, obtaining a stream F2 being depleted, compared to F1, in one or more of the one or more organic compounds comprising conjugated double bonds and the one or more chlorinated organic compounds; wherein (iii) comprises

[0117] (111.1) optionally subjecting the stream F1 obtained according to (ii) to hydrogenation in at least one reaction zone ZH containing a heterogeneous hydrogenation catalyst, ZH being comprised in ZP, obtaining a stream FH being depleted, compared to F1, in the one or more organic compounds comprising conjugated double bonds;

[0118] (111.2) subjecting the stream F1 obtained according to (ii), or FH obtained according to (iii.1 ), to dechlorination in at least one dechlorination zone ZD comprised in ZP, and located downstream of ZH if present, obtaining a stream F2 being depleted, compared to F1 , or FH when (iii.1) is performed, in the one or more chlorinated organic compounds.

[0119] Preferably, according to an alternative, the dehalogenation zone ZD according to (iii.2) comprises, more preferably is an adsorption zone, more preferably comprising a heterogeneous ad- sorbent material suitable for adsorbing halide comprised in at least one of the one or more halogenated organic compounds, more preferably in all of the one or more halogenated organic compounds.

[0120] Preferably, the heterogeneous adsorbent material according to (iii.2) comprises one or more of a carbon-containing adsorbent material and an aluminum-containing adsorbent material, more preferably an aluminum-containing adsorbent material. Preferably, the carbon-containing adsorbent material is a carbon-containing molecular sieve, more preferably activated charcoal.

[0121] Preferably, the aluminum-containing adsorbent material is an alumina, an aluminum-containing molecular sieve, a silicoaluminophosphate, a silica-alumina hydrate or a hydrotalcite; wherein the aluminum-containing molecular sieve is more preferably an alumina, an aluminosilicate, more preferably having a molar ratio of Si: Al, calculated as SiC^AhOs, in the range of from 2:1 to 10:1 , more preferably from 2:1 to 4:1 ; wherein the silica-alumina hydrate more preferably has weight ratio AhO3:SiO2 in the range of from 1 :1 to 10:1 , more preferably from 1 :1 to 2:1 ; wherein the hydrotalcite is more preferably an aluminum and magnesium containing hydrotalcite, more preferably an aluminum-magnesium hydroxycarbonate, more preferably having a MgOAhCh weight ratio in the range of from 63:37 to 70:30. More preferably, the heterogeneous adsorbent material more preferably comprises the hydrotalcite.

[0122] Preferably, the heterogeneous adsorbent material according to (iii.2) comprises an element of the groups 1 , 2, 11 and 12.

[0123] Preferably, the heterogeneous adsorbent material according to (iii.2) comprises particles characterized by a particle size distribution having a D50 value in the range of from 1 to 6,500 micrometers, more preferably from 2 to 2,000 micrometers, more preferably from 8 to 500 micrometers, more preferably from 10 to 50 micrometers or from 3 to 9 micrometers, the D50 particle size being determined as described in Reference Example 10.

[0124] Preferably, the heterogeneous adsorbent material according to (iii.2) has an average pore volume in the range of from 0.1 to 5 ml / g, more preferably in the range of from 0.15 to 2 ml / g, the average pore volume being determined as described in Reference Example 11.

[0125] Preferably, the heterogeneous adsorbent material according to (iii.2) has a BET specific surface area in the range of from 50 to 1 ,000 m2 / g, more preferably in the range of from 100 to 900 m2 / g, more preferably in the range of from 150 to 600 m2 / g, the BET specific surface area being determined as described in reference Example 12. Preferably, (iii.2) comprises

[0126] (111.2.1) introducing a gas stream G1 into ZD, more preferably being an adsorption zone, preferably a gas stream G1 comprising one or more of hydrogen and nitrogen, more preferably hydrogen;

[0127] (111.2.2) introducing the stream F1 obtained from (ii), or FH obtained in (iii.1 ), into ZD;

[0128] (111.2.3) bringing F1 , or FH, in contact with G1 and optionally a heterogeneous adsorbent material comprised in ZD, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds;

[0129] (111.2.4) removing F2 from ZD.

[0130] Preferably, the gas stream G1 has a temperature in the range of 100 to 500 °C, more preferably in the range of from 150 to 500°C, more preferably in the range of from 300 to 400 °C.

[0131] Preferably, the gas stream G1 is introduced at a pressure in the range of from 1 to 100 bar(abs), more preferably in the range of from 5 to 80 bar(abs), more preferably in the range of from 10 to 50 bar(abs).

[0132] Preferably, in ZD, the liquid hourly space velocity (LHSV) is in the range of from 0.2 to 10 h’1, more preferably in the range of from 0.3 to 5 h’1, more preferably in the range of from 0.5 to 2 IT 1

[0133] Preferably from 90 to 100 weight-%, more preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, of the gas stream G1 consists of H2. Alternatively, preferably from 90 to 100 weight-%, preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, of the gas stream G1 consists of nitrogen. Alternatively, preferably from 98 to 100 weight-% of G1 consists of nitrogen and hydrogen, wherein from 90 to 100 weight of G1 consists of nitrogen and from 0 to 10 weight% of G1 consists of hydrogen.

[0134] In the context of the present invention, preferably, according to (iii.2.1), G1 is introduced continuously or semi-continuously, more preferably continuously, into ZD and preferably according to (iii.2.2) F1 , or FH, is introduced continuously or semi-continuously, more preferably continuously, into ZD.

[0135] Preferably, the adsorption zone ZD is comprised in a continuous stirred tank reactor (CSTR), a fluidized bed or a fixed bed reactor, more preferably in a fixed bed reactor, the reactor more preferably comprising an adsorption bed comprising the heterogeneous adsorbent material. Preferably, according to (iii.2), two or more reaction zones Zo are employed which are arranged serially and / or in parallel, wherein more preferably, one single reaction zone ZD is employed according to (iii.2).

[0136] Preferably, the stream F2 obtained from (iii.2) has a total acid number (TAN) in the range of from 0 to 20 mg KOH / g, more preferably in the range of from 0 to 4.5 mg KOH / g, determined as described in Reference Example 1.

[0137] Preferably, the stream F2 obtained from (iii.2) has an oxygen content in the range of from 0 to 2 g(C>2) per 100g of the stream F2, determined as described in Reference Example 5.

[0138] Preferably, the stream F2 obtained from (iii.2) has a total chlorine content in the range of from 0 to 200 wppm (ppm by weight), more preferably from 0 to 160 wppm, more preferably from 0 to 130 wppm, more preferably from 0 to 120 wppm, determined as described in Reference Example 3.1.

[0139] Preferably, the stream F2 obtained from (iii.2) has a chloride content of at most 40 wppm (ppm by weight), more preferably from 0 to 30 wppm, more preferably from 0 to 20 wppm, more preferably from 0 to 1 wppm, determined as described in Reference Example 3.2.

[0140] Preferably, the stream F2 obtained from (iii.2) comprises the one or more organic compounds comprising conjugated double bonds in a total amount in the range of 0 to 3 g(l2) / 100 g, preferably from 0 to 2 g(l2) / 100 g, more preferably from 0 to 1 g(l2) / 100 g, more preferably from 0 to 0.25 g(l2) / 100 g, more preferably from 0 to 0.1 g(l2) / 100 g of the stream F2, determined as described in Reference Example 4.

[0141] Preferably, the stream F2 obtained from (iii.2) has a nitrogen content in the range of from 50 to 20,000 ppm by weight wppm, more preferably from 50 to 5,000 wppm, more preferably from 100 to 4,000 wppm, determined as described in Reference Example 2.

[0142] Preferably, the stream F2 obtained from (iii.2) has a sulfur content in the range of from 50 to 30,000 ppm by weight (wppm), more preferably from 50 to 5,000 wppm, more preferably from 100 to 3,000 wppm, determined as described in Reference Example 6.

[0143] Preferably, from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, more preferably from 99 to 100 weight-%, more preferably from 99.5 to 100 weight-%, of F2 consist of pyrolysis oil. Preferably, according to a further alternative, the dehalogenation zone ZD according to (iii.2) comprises, more preferably is a catalytic zone, more preferably comprising a heterogeneous dehalogenation catalyst, said catalyst comprising one or more catalytically active elements of groups 8 to 12 of the periodic system of elements.

[0144] Preferably, according to said alternative, (iii.2) comprising bringing in contact F1 , or FH obtained according to (iii.1 ), a heterogeneous dehalogenation catalyst, said catalyst comprising one or more catalytically active elements of groups 8 to 12 of the periodic system of elements, in ZD and reacting F1 or FH with said catalyst, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds.

[0145] Preferably, according to a further alternative, the dehalogenation according to (iii.2) comprises (iii.2. T) optionally introducing a gas stream G11 into ZD, being a reactor which is free of any adsorbent material and free of any catalyst, preferably the gas stream G11 comprising one or more of hydrogen and nitrogen, more preferably hydrogen;

[0146] (iii.2.2’) introducing the stream F1 obtained from (ii), or FH obtained in (iii.1 ), into ZD, being a reactor which is free of any adsorbent material and free of any catalyst;

[0147] (iii.2.3’) heating F1 , or FH, into the reactor and bringing in contact F1 , or FH, with G11 , if

[0148] (iii.2. T) is performed, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds;

[0149] (iii.2.4’) removing F2 from ZD.

[0150] According to said alternative for dehalogentation, preferably dechlorination, it is even not necessary to contact the extracted pyrolysis oil comprised in F1 or FH to a catalyst or an adsorbant material. The dechlorination preferably consists of a thermal treatment, preferably at a temperature in the range of from 200 to 400 °C.

[0151] Preferably, the gas stream G11 has a temperature in the range of 150 to 500°C, more preferably in the range of from 200 to 400 °C.

[0152] Preferably, the gas stream G11 is introduced at a pressure in the range of from 1 to 100 bar(abs), more preferably in the range of from 5 to 80 bar(abs), more preferably in the range of from 10 to 50 bar(abs).

[0153] Hydrogenation

[0154] Preferably, the stream F1 subjected to hydrogenation in (iii.1) has a temperature in the range of from 80 to 250 °C, more preferably from 90 to 220 °C, more preferably from 100 to 200 °C. Preferably, the heterogeneous hydrogenation catalyst according to (iii.1) comprises an element of the groups 8 to 12, more preferably 8 to 10, more preferably 9 and 10, of the periodic table of elements, preferably an element selected from the group consisting of Ni, Pd and Co, more preferably from the group consisting of Ni and Pd.

[0155] Preferably, the heterogeneous hydrogenation catalyst according to (iii.1) further comprises a support material for said element of the groups 8 to 12 of the periodic table of elements, wherein the support material is more preferably selected from the group consisting of an oxidic material and carbon, wherein the oxidic material is more preferably one or more of alumina, silica, magnesia, zirconia, titania, a zeolitic material, a silica-alumina phosphate (SAPO) material, zinc oxide, sodium oxide, mixed silica-alumina, zeolite and calcium oxide, more preferably alumina.

[0156] Preferably, the heterogeneous hydrogenation catalyst according to (iii.1) comprises Ni, more preferably in an amount, calculated as NiO, in the range of from 0.5 to 70 weight-%, more preferably from 0.75 to 45 weight-%, more preferably from 1 to 20 weight-%, based on the total weight of the hydrogenation catalyst.

[0157] Preferably, the heterogeneous hydrogenation catalyst used in (iii.1) further comprises an element of the group 6 of the periodic table of elements, wherein the element of the group 6 is preferably one or more of Mo and W, more preferably Mo.

[0158] Preferably, the hydrogenation catalyst comprises from 1 to 40 weight-%, more preferably from 2 to 35 weight-%, more preferably from 3 to 30 weight-% of said element of the group 6, based on the total weight of the hydrogenation catalyst.

[0159] Preferably, the heterogeneous hydrogenation catalyst according to (iii.1) comprises Ni and Mo supported on a support material, more preferably a support material as defined in the foregoing, wherein the hydrogenation catalyst preferably comprises Ni and Mo supported on alumina.

[0160] Alternatively, the heterogeneous hydrogenation catalyst according to (iii.1) comprises Pd, more preferably in an amount, calculated as elemental Pd, in the range of from 0.01 to 5 weight-%, more preferably from 0.1 to 1 weight-%, more preferably from 0.15 to 0.8 weight-%, based on the total weight of the catalyst. More preferably the heterogeneous hydrogenation catalyst according to (iii.1) further comprises a promoter, the promoter more preferably being one or more of an element of the groups 10 and 11 of the periodic table of elements, more preferably one or more of Cu, Au, Ag, and Pt, more preferably one or more of Ag and Pt, more preferably Ag. Preferably the atomic ratio of the element of groups 8 to 12 of the periodic table, more preferably Pd, relative to the promoter is in the range of from 0.1 :1 to 10:1 , more preferably from 2:1 to 7:1 , more preferably from 2.5:1 to 6:1.

[0161] Preferably, the heterogeneous hydrogenation catalyst according to (iii.1) comprises Pd supported on a support material, more preferably a support material as defined in the foregoing, wherein the support material is more preferably alumina or carbon, more preferably alumina.

[0162] In the context of the present invention, preferably, the heterogeneous hydrogenation catalyst according to (iii.1) is in the form of extrudates, pellets, rings, spherical particles or spheres, more preferably spherical particles or extrudates.

[0163] Preferably, (iii.1) comprises

[0164] (111.1.1) introducing a gas stream GO into ZH, the gas stream comprising H2;

[0165] (111.1.2) introducing the stream F1 into ZH;

[0166] (111.1.3) bringing F1 in contact with GO and the heterogeneous hydrogenation catalyst comprised in ZH, obtaining a stream FH being depleted, compared to F1 , in the one or more organic compounds comprising conjugated double bonds;

[0167] (111.1.4) removing FH from ZH.

[0168] (111.1.5) optionally removing a gas stream G1 from ZH, G1 comprising H2.

[0169] Preferably, the gas stream GO has a temperature in the range of 100 to 250 °C, more preferably from 120 to 220 °C, more preferably from 140 to 200 °C.

[0170] Preferably, the gas stream GO is introduced at a pressure in the range of from 10 to 100 bar(abs), more preferably from 15 to 90 bar(abs), more preferably from 20 to 80 bar(abs), more preferably in the range of from 20 to 55 bar(abs).

[0171] Preferably from 70 to 100 volume-%, more preferably from 80 to 100 volume-%, more preferably from 90 to 100 volume-%, of the gas stream GO consists of H2.

[0172] Preferably, according to (iii.1.1), GO is introduced continuously or semi-continuously, more preferably continuously into ZH, and preferably according to (iii.1.2), F1 is introduced semi-continu- ously or continuously, more preferably continuously, into ZH.

[0173] Preferably, GO is introduced into ZH according to (iii.1.1) for a period At prior to introducing F1 into Z1 according to (iii.1.2); wherein more preferably during At, GO is brought in contact with the heterogeneous hydrogenation catalyst comprised in ZH, wherein GO has a temperature in the range of 50 to 250 °C, more preferably from 120 to 220 °C, more preferably from 140 to 200 °C.

[0174] Preferably, in ZH, the liquid hourly space velocity (LHSV) is in the range of from 0.2 to 10 m3 / (m3h), more preferably in the range of from 0.3 to 5 m3 / (m3h), more preferably in the range of from 0.5 to 2 m3 / (m3h), wherein the LHSV is defined as the volume flow of F1 through ZH (in m3 / h) per volume of heterogeneous hydrogenation catalyst comprised in ZH (in m3).

[0175] Preferably, the reaction zone ZH is comprised in a continuous stirred tank reactor (CSTR) or a fixed bed reactor, more preferably in a fixed bed reactor, wherein the fixed bed reactor is more preferably a trickle bed reactor.

[0176] Preferably, according to (iii.1), two or more reaction zones ZH are employed which are arranged serially and / or in parallel, or wherein one single reaction zone ZH is employed according to (iii.1).

[0177] Preferably, the stream FH obtained from (iii.1) and subjected to dehalogenation in (iii.2) comprises the one or more organic compounds comprising conjugated double bonds in a total amount in the range of from 0 to 3 g(l2) / 100 g, more preferably from 0 to 2 g(l2) / 100g, more preferably from 0 to 1 g(l2) / 100 g, more preferably from 0 to 0.25 g(l2) / 100 g, more preferably from 0 to 0.1 g(l2) / 100 g of the stream FH, determined as described in Reference Example 4.

[0178] Preferably, the stream FH obtained from (iii.1), and subjected to dehalogenation in (iii.2), comprises a reduced styrene amount from 50 to 100%, more preferably from 70 to 100 %, more preferably from 75 to 100 %, compared to F0. The styrene amount is determined as described in Reference Example 7.

[0179] Preferably, the stream FH obtained from (iii.1) and subjected to dehalogenation in (iii.2) has a styrene content in the range of from 0 to 1 .5 Area%, more preferably in the range of from 0 to 0.1 Area%, determined as described in Reference Example 7.

[0180] Preferably, the stream FH subjected to dehalogenation in (iii.2) has a temperature in the range of from 150 to 450°C, more preferably from 200 to 400°C, more preferably from 250 to 350 °C.

[0181] Preferably, (iii) comprises

[0182] (iii.1’) subjecting the stream F1 obtained according to (ii) to distillation in at least one distillation zone ZL, ZL being comprised in ZP, obtaining a stream F2 being depleted, compared to F1 , in the one or more organic compounds and a stream F3 being enriched, compared to F1 , in the one or more organic compounds.

[0183] Preferably, the thermal treatment according to (iii.1’) is performed in a distillation column, wherein the stream F1 obtained according to (ii) depletes in two streams, F2 and F3. One of F2 and F3 comprising low and / or medium boiling components, obtained from the top of the column and the other of F2 and F3 comprising the heavy boiling components obtained from the bottom of the column. Additionally, a side stream may be withdrawn from the distillation column to obtain medium boiling components according to the predetermined specifications.

[0184] Preferably, distillation according to (iii.1 ’) is carried out at temperatures in the range of from 0 °C to 400 °C, more preferably from 60 °C to 400°C, more preferably from 80 °C to 250°C. The corresponding operating pressure of the distillation column according to (iii.T) is preferably in the range from 0.001 bar to 4 bar(abs), more preferably from 0.001 to 0.98 bar (abs), more preferably from 0.01 bar to 0.05 bar (abs).

[0185] Preferably, the predetermined top product specification and yield is obtained in one distillation column or a series of distillation columns, wherein the first distillation column is operated at pressure > 0.98 bar (abs) to recover the low boiling components which might otherwise be difficult to recover under lower pressures.

[0186] Step (iv)

[0187] Storage

[0188] Preferably, the process of the present invention further comprises

[0189] (iv) passing the stream F2 in a storage tank and storing the pyrolysis oil comprised in F2 for a duration AT, prior to one or more purification steps.

[0190] - Hydroprocessing

[0191] Alternatively, preferably, the process of the present invention further comprises

[0192] (iv) subjecting the stream F2 obtained from (iii) to hydroprocessing in at least one reaction zone ZHP downstream of ZD, ZHP comprising a heterogeneous hydroprocessing catalyst; obtaining a stream F3; wherein the stream F2 subjected to (iv) has a temperature in the range of from 150 to 400°C, more preferably in the range of from 200 to 375 °C, more preferably in the range of from 250 to 350 °C.

[0193] Preferably, the heterogeneous hydroprocessing catalyst used in (iv) comprises an element of the groups 8 to 10, preferably 9 and 10 of the periodic table of elements, preferably an element selected from the group consisting of Ni and Co, wherein the hydroprocessing catalyst more preferably comprises Ni; wherein the heterogeneous hydroprocessing catalyst according to (iv) more preferably comprises Ni in an amount, calculated as NiO, in the range of from 0.5 to 10 weight-%, more preferably in the range of from 1 to 6 weight-%, based on the weight of the hydroprocessing catalyst.

[0194] Preferably, the heterogeneous hydroprocessing catalyst according to (iv) further comprises a support for the element of the groups 8 to 10 of the periodic table of elements, wherein the support more preferably is an oxidic material. More preferably, the oxidic material is one or more of alumina, silica, magnesia, zirconia, zinc oxide, calcium oxide, mixed silica-alumina, zeolite, Mo- doped alumina and titania, more preferably alumina, zeolite and silica-alumina, more preferably alumina.

[0195] Preferably, the heterogeneous hydroprocessing catalyst according to (iv) further comprises an element of the group 6 of the periodic table of elements, wherein the element of the group 6 is preferably one or more of Mo and W. More preferably, the hydroprocessing catalyst comprises in the range of from 1 to 40 weight-%, more preferably from 3 to 30 weight-%, of an oxide of said element of the group 6, preferably Mo oxide or W oxide, based on the weight of the hydroprocessing catalyst.

[0196] Preferably, the heterogeneous hydroprocessing catalyst according to (iv) comprises Ni and Mo on a support, more preferably a support as defined in the foregoing, more preferably the support being one or more of alumina, zeolite and silica-alumina. More preferably, the hydroprocessing catalyst according to (iv) comprises Ni and Mo on alumina.

[0197] Preferably, (iv) comprises

[0198] (iv.1 ) introducing a gas stream G2 into ZHP, G2 comprising H2;

[0199] (iv.2) introducing the stream F2 obtained from (iii) into ZHP;

[0200] (iv.3) bringing F2 in contact with G2 and a heterogeneous hydroprocessing catalyst comprised in ZHP, obtaining a stream F3;

[0201] (iv.4) removing F3 obtained in (iv.3) from ZHP. Preferably, the gas stream G2 has a temperature in the range of 250 to 550°C, more preferably in the range of from 300 to 450 °C, more preferably in the range of from 325 to 400 °C.

[0202] Preferably, the gas stream G2 is introduced at a pressure in the range of from 20 to 150 bar (abs), more preferably in the range of from 30 to 90 bar(abs), more preferably in the range of from 40 to 80 bar(abs), more preferably in the range of from 45 to 60 bar(abs).

[0203] Preferably, in ZHP the liquid hourly space velocity (LHSV) is in the range of from 0.1 to 10 h’1, more preferably in the range of from 0.1 to 5 h’1, more preferably in the range of from 0.2 to 2 IT 1

[0204] Preferably, from 50 to 100 weight-%, more preferably from 70 to 100 weight-%, more preferably from 90 to 100 weight-%, of the gas stream G2 consists of H2.

[0205] Preferably, according to (iv.1 ) G2 is introduced continuously or semi-continuously, preferably continuously, into ZHP.

[0206] Preferably, according to (iv.2) F2 is introduced continuously or semi-continuously, more preferably continuously, into ZHP.

[0207] Preferably, the reaction zone ZHP is comprised in a reactor, more preferably comprising n serially coupled catalyst beds B(i), i= 1... , n, n > 2, wherein a catalyst bed B(i) comprises a heterogeneous hydroprocessing catalyst, more preferably 2 < n < 10, more preferably 2 < n < 5; wherein B(1) is the most upstream catalyst bed and B(n) is the most downstream catalyst bed.

[0208] Preferably, (iv) comprises

[0209] (iv.T) introducing a gas stream G2 into ZHP, G2 comprising H2;

[0210] (iv.2’) introducing the stream F2 obtained from (iii) into ZHP;

[0211] (iv.3’) n successive process stages P(i), i=1...n, wherein in P(1)

[0212] - the gas stream G2 is introduced into a catalyst bed B(1) and brought in contact with the stream F2 obtained from (iv) and a heterogeneous hydroprocessing catalyst in B(1), obtaining a stream SP(1 ); wherein in each P(i), when i=2... n-1 , a gas stream X(i-1), comprising H2, is introduced into a catalyst bed B(i) and brought in contact with Sp(i-1) and a heterogeneous hydroprocessing catalyst in B(i), obtaining a stream Sp(i); removing Sp(i) from B(i); and wherein in P(n), a gas stream X(n-1) is introduced into a catalyst bed B(n) and brought in contact with Sp(n-1) and a heterogeneous hydroprocessing catalyst in B(n), obtaining a gas stream F3;

[0213] (iv.4’) removing F3 obtained in (iv.3’) from ZHP.

[0214] Preferably, the gas stream G2 has a temperature in the range of 250 to 550°C, more preferably in the range of from 300 to 450 °C, more preferably in the range of from 325 to 400 °C.

[0215] Preferably, the gas stream G2 is introduced at a pressure in the range of from 20 to 150 bar (abs), more preferably in the range of from 30 to 90 bar(abs), more preferably in the range of from 40 to 80 bar (abs), more preferably in the range of from 45 to 60 bar(abs).

[0216] Preferably, from 50 to 100 weight-%, more preferably from 70 to 100 weight-%, more preferably from 90 to 100 weight-%, of the gas stream G2 consists of H2.

[0217] Preferably, in ZHP, the liquid hourly space velocity (LHSV) is in the range of from 0.1 to 10 h’1, more preferably in the range of from 0.1 to 5 h’1, more preferably in the range of from 0.2 to 2 IT 1

[0218] Preferably, according to (iv.T), G2 is introduced continuously or semi-continuously, more preferably continuously, into ZHP.

[0219] Preferably, according to (iv.2’), F2 is introduced continuously or semi-continuously, more preferably continuously, into ZHP.

[0220] Preferably, from 50 to 100 weight-%, more preferably from 70 to 100 weight-%, more preferably from 90 to 100 weight-%, of the gas stream X(i) consists of H2.

[0221] Preferably, the gas stream X(i) is introduced at a pressure in the range of from 20 to 150 bar(abs), more preferably in the range of from 30 to 90 bar(abs), more preferably in the range of from 40 to 80 bar (abs), more preferably in the range of from 45 to 60 bar(abs).

[0222] Preferably, the n serially coupled catalyst bed B(i) are fixed catalyst beds.

[0223] Preferably, the reaction zone ZHP is comprised in a continuous stirred tank reactor (CSTR) or a fixed bed reactor, more preferably in a fixed bed reactor, more preferably a trickle bed reactor. Preferably, the stream F3 obtained from (iv) has a total acid number (TAN) in the range of from 0 to 10 mg KOH / g(F3), more preferably in the range of from 0 to 4.5 mg KOH / g(F3), determined as described in Reference Example 1.

[0224] Preferably, the stream F3 obtained from (iv) has an oxygen content in the range of from 0 to 2 g(0) / 100g(F3), determined as described in Reference Example 5.

[0225] Preferably, the stream F3 obtained from (iv) has a total chlorine content in the range of from 0 to 50 wppm (ppm by weight), more preferably from 0 to 30 wppm, more preferably from 0 to 20 wppm, more preferably from 0 to 10 wppm, more preferably from 0 to 5 wppm, more preferably from 0 to less than 2 wppm, determined as described in Reference Example 3.1.

[0226] Preferably, the stream F3 obtained from (iv), more preferably after removing dissolved NH3, has a nitrogen content in the range of from 0 to 200 ppm by weight (wppm), more preferably in the range of from 0 to 100 wppm, more preferably from 0 to 50 wppm, more preferably from 0 to 10 wppm, determined as described in Reference Example 2.

[0227] Preferably, the stream F3 obtained from (iv), more preferably after removing dissolved H2S, has a sulfur content in the range of from 0 to 200 ppm by weight (wppm), more preferably from 0 to 100 wppm, more preferably from 0 to 50 wppm, determined as described in Reference Example 6.

[0228] Preferably, the stream F3 obtained from (iv) comprises the one or more organic compounds comprising conjugated double bonds in a total amount in the range of 0 to 3 g(l2) / 100 g, more preferably from 0 to 2 g(l2) / 100 g, more preferably from 0 to 1 g(l2) / 100 g, more preferably from 0 to 0.25 g(l2) / 100 g, more preferably from 0 to 0.1 g(l2) / 100 g of the stream F3 obtained from (iv), determined as described in Reference Example 4.

[0229] Other steps

[0230] Preferably, the process further comprises, after (iii) one or more of a steam cracking step, a hydrocracking step, an hydroprocessing step, a distillation step, a stripping step, a storage step, and an aqueous extraction step.

[0231] Preferably, the process of the present invention is a continuous or semi-continuous process.

[0232] Preferably, the process according to the present invention consists of (i), (ii) and (iii), more preferably (i), (ii), (iii) and (iv). The present invention further relates to a production unit for carrying out the process for purifying a pyrolysis oil according to the present invention, the unit comprising an inlet means for introducing F0 into ZE; an outlet means for removing F1 from ZE; at least one extraction zone ZE, at least one thermal treating zone ZP, ZP being located downstream of ZE; an inlet means for introducing F1 into ZP; an outlet means for removing F2 from ZD.

[0233] Preferably, the unit comprises optionally at least one reaction zone ZH containing a heterogeneous hydrogenation catalyst, ZH being comprised in ZP, optionally an inlet means for introducing F1 into ZH; optionally an outlet means for removing FH from ZH; at least one dehalogenation zone ZD comprised in ZP and downstream of ZH if present, wherein ZD preferably comprising a heterogeneous adsorption material or a heterogeneous dehalogenation catalyst or is free of any catalyst and any adsorption material; an inlet means for introducing F1, or Fnwhen ZH is present, into ZD, preferably ZP = ZD + optionally ZH.

[0234] Preferably, the unit further comprises at least one distillation zone ZL, ZL being comprised in ZP; an inlet means for introducing F1 into ZL, preferably ZL= ZP.

[0235] Preferably, the unit further comprises at least one reaction zone ZHP, ZHP comprising a heterogeneous hydroprocessing catalyst; an inlet means for introducing F2 into ZHP; an outlet means for removing F3 from ZHP; wherein ZP is located upstream of ZHP.

[0236] The present invention further relates to a purified pyrolysis oil, obtainable or obtained by a process according to the present invention.

[0237] Preferably, the purified pyrolysis oil of the present invention has a total acid number (TAN) in the range of from 0 to 10 mg KOH / g(oil), more preferably in the range of from 0 to 4.5 mg KOH / g(oil), determined as described in Reference Example 1. Preferably, the purified pyrolysis oil of the present invention has an oxygen content in the range of from 0 to 2 g(O) / 1 OOg(oil), determined as described in Reference Example 5.

[0238] Preferably, the purified pyrolysis oil of the present invention has a nitrogen content in the range of from 10 to 20,000 wppm (ppm by weight), more preferably from 50 to 5,000 wppm, more preferably from 100 to 4000 wppm , determined as described in Reference Example 2.

[0239] 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 one of embodiments 1 to 4", 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 one of embodiments 1 , 2, 3 and 4". Further, it is explicitly noted that the following set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.

[0240] 1 . A process for purifying a pyrolysis oil, the process comprising:

[0241] (i) providing a stream F0 comprising a pyrolysis oil, the pyrolysis oil comprising one or more halogenated organic compounds and one or more organic compounds comprising conjugated double bonds;

[0242] (ii) subjecting the stream F0 provided in (i) to extraction in at least one extraction zone ZE, obtaining a stream F1 comprising the extracted pyrolysis oil, wherein (ii) comprises:

[0243] (ii.1 ) introducing F0 into ZE;

[0244] (11.2) bringing in contact F0 with water and a base B into ZE at a temperature in the range of from 10 to 200 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 ;

[0245] (11.3) separating PA from Po, obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil;

[0246] (iii) subjecting the stream F1 obtained according to (ii) to thermal treatment in at least one thermal treating zone ZP, ZP being located downstream of ZE, obtaining a stream F2 being depleted, compared to F1 , in one or more of the one or more organic compounds comprising conjugated double bonds and the one or more halogenated organic compounds. The process of embodiment 1, wherein the thermal treatment according to (iii) is performed at a temperature in the range of from 80 to 400 °C. The process of embodiment 1 or 2, wherein the pyrolysis oil according to (i) has an oxygen content in the range of from 0.1 to 15 g(O) / 100g(F0), preferably in the range of from 0.5 to 10 g(O) / 100g(F0), more preferably in the range of from 0.1 to 5 g(O) / 100g(F0) determined as described in Reference Example 5. The process of any one of embodiments 1 to 3, wherein the pyrolysis oil according to (i) has a total acid number (TAN) in the range of from 0.5 to 60 mg KOH / g(F0), preferably in the range of from 1 to 40 mg KOH / g(F0), more preferably in the range of from 3 to 20 mg KOH / g(F0) determined as described in Reference Example 1. The process of any one of embodiments 1 to 4, wherein the one or more halogenated organic compounds comprised in the pyrolysis oil according to (i) comprise one or more of mono- oligo- or polyhalogenated aromatic compounds, alkylhalides and alkenylhalides. The process of any one of embodiments 1 to 5, wherein the pyrolysis oil according to (i) has a total chlorine content in the range of from 30 to 3,000 wppm (ppm by weight), preferably from 30 to 500 wppm, more preferably from 30 to 100 wppm, determined as described in Reference Example 3.1. The process of any one of embodiments 1 to 6, wherein the pyrolysis oil according to (i) has a nitrogen content in the range of from 10 to 20,000 wppm (ppm by weight), preferably from 50 to 5,000 wppm, more preferably from 100 to 4,000 wppm, determined as described in Reference Example 2. The process of any one of embodiments 1 to 7, wherein the pyrolysis oil according to (i) has a sulfur content in the range of from 10 to 30,000 ppm by weight (wppm), preferably from 20 to 5,000 wppm, more preferably from 50 to 3,000 wppm, determined as described in Reference Example 6. The process of any one of embodiments 1 to 8, wherein the pyrolysis oil according to (i) comprises the one or more organic compounds comprising conjugated double bonds in a total amount in the range of from 0.1 to 75 g(l2) / 100 g, preferably from 0.4 to 60 g(l2) / 100 g, more preferably from 1 to 30 g(l2) / 100 g of the pyrolysis oil, determined as described in Reference Example 4; and / or wherein the pyrolysis oil according to (i) has a styrene content in the range of from 0.2 to 30 Area%, more preferably in the range of from 1 to 20 Area%, determined as described in Reference Example 7.

[0247] 10. The process of any one of embodiments 1 to 9, wherein the one or more organic compounds comprising conjugated double bonds comprise one or more organic compounds according to formula (I)

[0248] R1R2C1=C2R3-C3R4=X (I) wherein =X is =0, =S, =NR5, or =C4R6R7, preferably =C4R6R7; preferably wherein R1, R2, R3, R4, R5are, independently of each other, H, alkyl having from 1 to 6 carbon atoms, alkenyl having from 1 to 6 carbon atoms, or aryl having from 5 to 10 carbon atoms, more preferably H; preferably wherein R6and R7are, independently of each other, H, alkyl having from 1 to 6 carbon atoms, alkenyl having from 1 to 6 carbon atoms, or aryl having from 5 to 10 carbon atoms, more preferably H; or preferably wherein either R4and R6or R4and R7are linked together, thus forming, together with C3=C4, an aromatic ring preferably having 5 or 6 members.

[0249] 11 . The process of any one of embodiments 1 to 10, wherein the pyrolysis oil is obtained from a waste material.

[0250] 12. The process of any one of embodiments 1 to 11 , wherein the stream F0 is a liquid stream.

[0251] 13. The process of any one of embodiments 1 to 12, wherein no organic solvent is used in the extraction according to (ii).

[0252] 14. The process of any one of embodiments 1 to 13, wherein the extraction according to (ii) is performed at a pressure PE in the range of from 0.8 to 1.2 bar(abs), more preferably in the range of from 0.9 to 1.1 bar(abs).

[0253] 15. The process of any one of embodiment 1 to 14, wherein the extraction according to (ii) is performed at a temperature in the range of from 10 to 95 °C, preferably in the range of from 15 to 90°C, more preferably in the range of from 20 to 85 °C, more preferably in the range of from 25 to 80 °C, more preferably in the range of from 30 to 70 °C, more preferably in the range of from 33 to 65 °C, more preferably in the range of from 35 to 60°C. 16. The process of any one of embodiments 1 to 15, wherein the base B is one or more of an alkali metal compound, an alkaline earth metal compound and ammonia, preferably B is an alkali metal compound being one or more of potassium hydroxide, sodium hydroxide, potassium carbonate, sodium carbonate, potassium bicarbonate and sodium bicarbonate, more preferably one or more of potassium hydroxide, sodium hydroxide, potassium carbonate and sodium carbonate, more preferably one or more of potassium hydroxide and sodium hydroxide, more preferably potassium hydroxide or sodium hydroxide, more preferably potassium hydroxide.

[0254] 17. The process of any one of embodiments 1 to 16, wherein for the extraction according to (ii), the weight ratio of water to F0 in ZE is in the range of from 0.05:1 to 2:1 , preferably in the range of from 0.1 :1 to 1.5:1, more preferably in the range of from 0.1:1 to 1.2:1 , more preferably in the range of from 0.1 :1 to 0.7:1 , more preferably in the range of from 0.2:1 to 0.5:1, more preferably in the range of from 0.3:1 to 0.5:1.

[0255] 18. The process of any one of embodiments 1 to 17, wherein the pH of the aqueous phase PA of M obtained according to (ii.2) is in the range of from 7 to 10.

[0256] 19. The process of any one of embodiments 1 to 18, wherein (ii.2) comprises

[0257] (11.2.1 ) introducing water and B, preferably a mixture of water and B, into ZE;

[0258] (11.2.2) bringing in contact, preferably mixing, F0 with water and B, preferably the mixture of water and B, into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , preferably in the range of from 7 to 10.

[0259] 20. The process of any one of embodiments 1 to 18, wherein (ii.2) comprises

[0260] (ii.2.1 ’) introducing water into ZE;

[0261] (ii.2.2’) bringing in contact, preferably mixing, F0 with water into ZE, obtaining a mixture comprising water and the pyrolysis oil;

[0262] (ii.2.3’) introducing B into ZE and bringing in contact, preferably mixing, B with the mixture obtained in (ii.2.2’) into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , preferably in the range of from 7 to 10.

[0263] 21. The process of embodiment 20, wherein (ii.2) comprises (ii.2.1 ’) introducing water into ZE; (ii .2.2’) bringing in contact, preferably mixing, F0 with water into ZE, obtaining a mixture M1 comprising water and the pyrolysis oil, wherein the pH of the aqueous phase of M1 has a pH, preferably measured by a pH-sensor in ZE;

[0264] (ii.2.3’) adjusting the pH of the aqueous phase of M1 by introducing B into ZE and bringing in contact, preferably mixing, B with M1 obtained in (ii.2.2’) into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, wherein the pH of the aqueous phase PA of M is in the range of from 7 to 11 and pH of the aqueous phase PA of M > pH of the aqueous phase of M1.

[0265] 22. The process of any one of embodiments 1 to 21, wherein (ii) comprises

[0266] (11.1) introducing F0 into a mixing unit UM1 comprised in ZE;

[0267] (11.2) mixing F0 with water and a base B into UM1 at a temperature in the range of from 10 to 200 °C, preferably from 10 to 95 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 ; removing M from UM1 ;

[0268] (11.3) separating PA from Po, wherein (ii.3) comprises

[0269] (ii.3.1) passing M into a liquid-liquid separation unit US1 comprised in ZE, US1 being located downstream of UM1 , obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil; removing F1 from ZE.

[0270] 23. The process of any one of embodiments 1 to 21, wherein (ii) comprises

[0271] (11.1) introducing F0 into a mixing unit UM1 comprised in ZE;

[0272] (11.2) mixing F0 with water and a base B into UM1 at a temperature in the range of from 10 to 200 °C, preferably from 10 to 95 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , more preferably in the range of from 7.5 to 11 ; removing M from UM1;

[0273] (11.3) separating PA from Po, wherein (ii.3) comprises

[0274] (ii.3.1 ’) passing M into a liquid-liquid separation unit US1 comprised in ZE, US1 being downstream of UM1, obtaining a stream FA comprising PA and a stream F1” comprising Po being the extracted pyrolysis oil; removing F1” from US1 ;

[0275] (ii.3.2’) subjecting the stream F1” provided in (ii.3.1’) to washing, obtaining a stream F1 comprising the extracted pyrolysis oil which has been purified, wherein (iii.3.2’) comprises: (A) introducing F1” into a mixing unit UM2 comprised in ZE, UM2 being located downstream of US1 in ZE; mixing F1” with water in UM2 at a temperature T2 in the range of from 10 to 95 °C, obtaining a mixture comprising an aqueous phase PA(2) and an organic phase Po(2), the pH of the aqueous phase PA(2) of M2 being in the range of from 7.5 to 11, pH of PA(2) < pH of PA; passing the obtained mixture into a liquid-liquid separation unit US2 comprised in ZE, US2 being located downstream of UM2, obtaining a stream F1 comprising the extracted pyrolysis oil which has been purified Po(2); or

[0276] (B)

[0277] - introducing F1” into an extraction column UM+IIS comprised in ZE;

[0278] - introducing water into UM+IIS;

[0279] - bringing in contact F1” with water in UM+IIS at a temperature T2’ in the range of from 10 to 95 °C, obtaining a stream FA(2) comprising an aqueous phase PA(2), the pH of the aqueous phase PA(2) of M2 being in the range of from 7.5 to 11 , pH of PA(2) < pH of PA, and obtaining a stream F1 comprising the extracted pyrolysis oil which has been purified Po(2). The process of any one of embodiments 1 to 23, wherein the thermal treatment according to (iii) is one or more of dehalogenation, hydrogenation, hydroprocessing, heat-up for dehalogenation, heat-up for hydrogenation, heat-up for hydroprocessing and distillation. The process of any one of embodiments 1 to 24, wherein (iii) comprises

[0280] (111.1) optionally subjecting the stream F1 obtained according to (ii) to hydrogenation in at least one reaction zone ZH containing a heterogeneous hydrogenation catalyst, ZH being comprised in ZP, obtaining a stream FH being depleted, compared to F1, in the one or more organic compounds comprising conjugated double bonds;

[0281] (111.2) subjecting the stream F1 obtained according to (ii), or FH obtained according to (iii.1 ), to dehalogenation in at least one dehalogenation zone ZD comprised in ZP, and located downstream of ZH if present, obtaining a stream F2 being depleted, compared to F1 , or FH when (iii.1) is performed, in the one or more halogenated organic compounds. The process of embodiment 25, wherein the dehalogenation zone ZD according to (iii.2) comprises, preferably is an adsorption zone, preferably comprising a heterogeneous adsorbent material suitable for adsorbing halide comprised in at least one of the one or more halogenated organic compounds, preferably in all of the one or more halogenated organic compounds. The process of embodiment 26, wherein the heterogeneous adsorbent material according to (iii.2) comprises one or more of a carbon-containing adsorbent material and an alumi- num-containing adsorbent material, preferably an aluminum-containing adsorbent material; wherein the carbon-containing adsorbent material is preferably a carbon-containing molecular sieve, more preferably activated charcoal; wherein the aluminum-containing adsorbent material is preferably an alumina, an aluminum-containing molecular sieve, a silicoaluminophosphate, a silica-alumina hydrate or a hydrotalcite; wherein the aluminum-containing molecular sieve is preferably an alumina, an aluminosilicate, preferably having a molar ratio of Si : Al, calculated as SiC^AhOs, in the range of from 2:1 to 10:1 , more preferably from 2:1 to 4:1 ; wherein the silica-alumina hydrate preferably has weight ratio AhO3:SiO2 in the range of from 1 :1 to 10:1 , more preferably from 1 :1 to 2:1 ; wherein the hydrotalcite is preferably an aluminum and magnesium containing hydrotalcite, more preferably an aluminum-magnesium hydroxycarbonate, preferably having a MgOAhCh weight ratio in the range of from 63:37 to 70:30; wherein the heterogeneous adsorbent material more preferably comprises the hydrotalcite; wherein the heterogeneous adsorbent material according to (iii.2) preferably comprises an element of the groups 1 , 2, 11 and 12. The process of any one of embodiments 25 to 27, wherein the heterogeneous adsorbent material according to (iii.2) comprises particles characterized by a particle size distribution having a D50 value in the range of from 1 to 6,500 micrometers, preferably from 2 to 2,000 micrometers, more preferably from 8 to 500 micrometers, more preferably from 10 to 50 micrometers or from 3 to 9 micrometers, the D50 particle size being determined as described in Reference Example 10. The process of any one of embodiments 25 to 27, wherein the heterogeneous adsorbent material according to (iii.2) has an average pore volume in the range of from 0.1 to 5 ml / g, preferably in the range of from 0.15 to 2 ml / g, the average pore volume being determined as described in Reference Example 11 . The process of any one of embodiments 25 to 28, wherein the heterogeneous adsorbent material according to (iii.2) has a BET specific surface area in the range of from 50 to 1 ,000 m2 / g, preferably in the range of from 100 to 900 m2 / g, more preferably in the range of from 150 to 600 m2 / g, the BET specific surface area being determined as described in reference Example 12. The process of any one of embodiments 25 to 30, wherein (iii.2) comprises

[0282] (111.2.1) introducing a gas stream G1 into ZD, preferably being an adsorption zone, preferably a gas stream G1 comprising one or more of hydrogen and nitrogen, more preferably hydrogen;

[0283] (111.2.2) introducing the stream F1 obtained from (ii), or FH obtained in (iii.1 ), into ZD;

[0284] (111.2.3) bringing F1 , or FH, in contact with G1 and optionally a heterogeneous adsorbent material comprised in ZD, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds;

[0285] (111.2.4) removing F2 from ZD. The process of embodiment 31 , wherein the gas stream G1 has a temperature in the range of 150 to 500°C, preferably in the range of from 300 to 400 °C. The process of embodiment 31 or 32, wherein the gas stream G1 is introduced at a pressure in the range of from 1 to 100 bar(abs), preferably in the range of from 5 to 80 bar(abs), more preferably in the range of from 10 to 50 bar(abs). The process of any one of embodiments 29 to 33, wherein in ZD, the liquid hourly space velocity (LHSV) is in the range of from 0.2 to 10 h’1, preferably in the range of from 0.3 to 5 h’1, more preferably in the range of from 0.5 to 2 h’1. The process of any one of embodiments 31 to 34, wherein from 90 to 100 weight-%, preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, of the gas stream G1 consists of H2; or wherein from 90 to 100 weight-%, preferably from 95 to 100 weight-%, more preferably from 98 to 100 weight-%, of the gas stream G1 consists of nitrogen; or wherein from 98 to 100 weight-% of G1 consists of nitrogen and hydrogen, wherein from 90 to 100 weight of G1 consists of nitrogen and from 0 to 10 weight% of G1 consists of hydrogen.

[0286] 36. The process of any one of embodiments 31 to 35, wherein according to (iii.2.1), G1 is introduced continuously or semi-continuously, preferably continuously, into ZD and wherein according to (iii.2.2) F1 , or FH, is introduced continuously or semi-continuously, preferably continuously, into ZD; wherein the adsorption zone ZD is preferably comprised in a continuous stirred tank reactor (CSTR), a fluidized bed or a fixed bed reactor, preferably in a fixed bed reactor, the reactor preferably comprising an adsorption bed comprising the heterogeneous adsorbent material.

[0287] 37. The process of any one of embodiments 25 to 36, wherein, according to (iii.2), two or more reaction zones Zo are employed which are arranged serially and / or in parallel, or wherein one single reaction zone ZD is employed according to (iii.2).

[0288] 38. The process of embodiment 25, wherein the dehalogenation zone ZD according to (iii.2) comprises, preferably is a catalytic zone, preferably comprising a heterogeneous dehalogenation catalyst, said catalyst comprising one or more catalytically active elements of groups 8 to 12 of the periodic system of elements.

[0289] 39. The process of embodiment 25, wherein dehalogenation according to (iii.2) comprises (iii.2. T) optionally introducing a gas stream G11 into ZD, being a reactor which is free of any adsorbent material and free of any catalyst, preferably the gas stream G11 comprising one or more of hydrogen and nitrogen, more preferably hydrogen;

[0290] (iii.2.2’) introducing the stream F1 obtained from (ii), or FH obtained in (iii.1 ), into ZD;

[0291] (iii.2.3’) heating F1 , or FH, into the reactor and bringing in contact F1 , or FH, with G11 , if (iii.2. T) is performed, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds;

[0292] (iii.2.4’) removing F2 from ZD.

[0293] 40. The process of any one of embodiments 25 to 39, wherein the stream F1 subjected to hydrogenation in (iii.1) has a temperature in the range of from 80 to 250 °C, preferably from 90 to 220 °C, more preferably from 100 to 200 °C. 41 . The process of any one of embodiments 25 to 40, wherein the heterogeneous hydrogenation catalyst according to (iii.1) comprises an element of the groups 8 to 12, preferably 8 to 10, more preferably 9 and 10, of the periodic table of elements, preferably an element selected from the group consisting of Ni, Pd and Co, more preferably from the group consisting of Ni and Pd.

[0294] 42. The process of embodiment 41 , wherein the heterogeneous hydrogenation catalyst according to (iii.1) further comprises a support material for said element of the groups 8 to 12 of the periodic table of elements, wherein the support material is preferably selected from the group consisting of an oxidic material and carbon, wherein the oxidic material is preferably one or more of alumina, silica, magnesia, zirconia, titania, a zeolitic material, a silica-alumina phosphate (SAPO) material, zinc oxide, sodium oxide, mixed silica-alumina, zeolite and calcium oxide, more preferably alumina.

[0295] 43. The process of embodiment 41 or 42, wherein the heterogeneous hydrogenation catalyst according to (iii.1) comprises Ni, preferably in an amount, calculated as NiO, in the range of from 0.5 to 70 weight-%, more preferably from 0.75 to 45 weight-%, more preferably from 1 to 20 weight-%, based on the total weight of the hydrogenation catalyst.

[0296] 44. The process of any one of embodiments 41 to 43, wherein the heterogeneous hydrogenation catalyst used in (iii.1) further comprises an element of the group 6 of the periodic table of elements, wherein the element of the group 6 is preferably one or more of Mo and W, more preferably Mo; wherein preferably the heterogeneous hydrogenation catalyst according to (iii.1) comprises Ni and Mo supported on a support material, preferably a support material as defined in embodiment 16, wherein the hydrogenation catalyst preferably comprises Ni and Mo supported on alumina; wherein the hydrogenation catalyst more preferably comprises from 1 to 40 weight-%, more preferably from 2 to 35 weight-%, more preferably from 3 to 30 weight-% of said element of the group 6, based on the total weight of the hydrogenation catalyst.

[0297] 45. The process of embodiment 41 or 42, wherein the heterogeneous hydrogenation catalyst according to (iii.1) comprises Pd, preferably in an amount, calculated as elemental Pd, in the range of from 0.01 to 5 weight-%, preferably from 0.1 to 1 weight-%, more preferably from 0.15 to 0.8 weight-%, based on the total weight of the catalyst; wherein preferably the heterogeneous hydrogenation catalyst according to (iii.1) further comprises a promoter, the promoter more preferably being one or more of an element of the groups 10 and 11 of the periodic table of elements, more preferably one or more of Cu, Au, Ag, and Pt, more preferably one or more of Ag and Pt, more preferably Ag; wherein more preferably the atomic ratio of the element of groups 8 to 12 of the periodic table, preferably Pd, relative to the promoter is in the range of from 0.1 :1 to 10:1 , more preferably from 2:1 to 7:1 , more preferably from 2.5:1 to 6:1.

[0298] 46. The process of embodiment 45, wherein the heterogeneous hydrogenation catalyst according to (iii.1) comprises Pd supported on a support material, preferably a support material as defined in embodiment 16, wherein the support material is preferably alumina or carbon, more preferably alumina.

[0299] 47. The process of any one of embodiments 25 to 46, wherein the heterogeneous hydrogenation catalyst according to (iii.1) is in the form of extrudates, pellets, rings, spherical particles or spheres, preferably spherical particles or extrudates.

[0300] 48. The process of any one of embodiments 25 to 47, wherein (iii.1) comprises

[0301] (111.1.1) introducing a gas stream GO into ZH, the gas stream comprising H2;

[0302] (111.1.2) introducing the stream F1 into ZH;

[0303] (111.1.3) bringing F1 in contact with GO and the heterogeneous hydrogenation catalyst comprised in ZH, obtaining a stream FH being depleted, compared to F1 , in the one or more organic compounds comprising conjugated double bonds;

[0304] (111.1 .4) removing FH from ZH.

[0305] (111.1.5) optionally removing a gas stream G1 from ZH, G1 comprising H2.

[0306] 49. The process of embodiment 48, wherein the gas stream GO has a temperature in the range of 100 to 250 °C, preferably from 120 to 220 °C, more preferably from 140 to 200 °C.

[0307] 50. The process of embodiment 48 or 49, wherein the gas stream GO is introduced at a pressure in the range of from 10 to 100 bar(abs), preferably from 15 to 90 bar(abs), more preferably from 20 to 80 bar(abs), more preferably in the range of from 20 to 55 bar(abs).

[0308] 51 . The process of any one of embodiments 48 to 50, wherein from 70 to 100 volume-%, preferably from 80 to 100 volume-%, more preferably from 90 to 100 volume-%, of the gas stream GO consists of H2.

[0309] 52. The process of any one of embodiments 48 to 51 , wherein according to (iii.1.1), GO is introduced continuously or semi-continuously, preferably continuously into ZH, and wherein according to (iii.1.2), F1 is introduced semi-continuously or continuously, preferably continuously, into ZH.

[0310] 53. The process of embodiment 52, wherein GO is introduced into ZH according to (iii.1.1) for a period At prior to introducing F1 into Z1 according to (iii.1.2); wherein preferably during At, GO is brought in contact with the heterogeneous hydrogenation catalyst comprised in ZH, wherein GO has a temperature in the range of 50 to 250 °C, more preferably from 120 to 220 °C, more preferably from 140 to 200 °C.

[0311] 54. The process of any one of embodiments 48 to 53, wherein in ZH, the liquid hourly space velocity (LHSV) is in the range of from 0.2 to 10 m3 / (m3h), preferably in the range of from 0.3 to 5 m3 / (m3h), more preferably in the range of from 0.5 to 2 m3 / (m3h), wherein the LHSV is defined as the volume flow of F1 through ZH (in m3 / h) per volume of heterogeneous hydrogenation catalyst comprised in ZH (in m3).

[0312] 55. The process of any one of embodiments 25 to 54, wherein the reaction zone ZH is comprised in a continuous stirred tank reactor (CSTR) or a fixed bed reactor, preferably in a fixed bed reactor, wherein the fixed bed reactor is preferably a trickle bed reactor.

[0313] 56. The process of any one of embodiments 25 to 55, wherein according to (iii.1 ), two or more reaction zones ZH are employed which are arranged serially and / or in parallel, or wherein one single reaction zone ZH is employed according to (iii.1).

[0314] 57. The process of any one of embodiments 25 to 56, wherein the stream FH subjected to dehalogenation in (iii.2) has a temperature in the range of from 150 to 450°C, preferably from 200 to 400°C, more preferably from 250 to 350 °C.

[0315] 58. The process of any one of embodiments 1 to 24, wherein (iii) comprises

[0316] (iii.T) subjecting the stream F1 obtained according to (ii) to distillation in at least one distillation zone ZL, ZL being comprised in ZP, obtaining a stream F2 being depleted, compared to F1 , in the one or more organic compounds and a stream F3 being enriched compared to F1 , in the one or more organic compounds.

[0317] 59. The process of any one of embodiments 1 to 58, further comprising, after (iii) one or more of a steam cracking step, a hydrocracking step, an hydroprocessing step, a distillation step, a stripping step, a storage step, and an aqueous extraction step. 60. The process of any one of embodiments 1 to 59, being a continuous or semi-continuous process.

[0318] 61. A production unit for carrying out the process for purifying a pyrolysis oil according to any one of embodiments 1 to 60, the unit comprising an inlet means for introducing F0 into ZE; an outlet means for removing F1 from ZE; at least one extraction zone ZE, at least one thermal treating zone ZP, ZP being located downstream of ZE; an inlet means for introducing F1 into ZP; an outlet means for removing F2 from ZD.

[0319] 62. The production unit of embodiment 61 , further comprising optionally at least one reaction zone ZH containing a heterogeneous hydrogenation catalyst, ZH being comprised in ZP, optionally an inlet means for introducing F1 into ZH; optionally an outlet means for removing FH from ZH; at least one dehalogenation zone ZD comprised in ZP and downstream of ZH if present, wherein ZD preferably comprising a heterogeneous adsorption material or a heterogeneous dehalogenation catalyst or is free of any catalyst and any adsorption material; an inlet means for introducing F1, or Fnwhen ZH is present, into ZD, preferably ZP = ZD + optionally ZH.

[0320] 63. The production unit of embodiment 61 , further comprising at least one distillation zone ZL, ZL being comprised in ZP; an inlet means for introducing F1 into ZL, preferably ZL= ZP.

[0321] 64. The production unit of any one of embodiments 61 to 63, further comprising at least one reaction zone ZHP, ZHP comprising a heterogeneous hydroprocessing catalyst; an inlet means for introducing F2 into ZHP; an outlet means for removing F3 from ZHP; wherein ZP is located upstream of ZHP.

[0322] 65. Process comprising the step: using the production unit according to any one of embodiments 61 to 64 to obtain a purified pyrolysis oil, monomer, polymer or polymer product. Process, preferably comprising the steps according to any one of embodiments 1 to 60, comprising the further step: converting the stream F2 obtainable or obtained by the process according to any one of embodiments 1 to 60 or a chemical material obtainable by or obtained by the process according to any one of embodiments 1 to 60 to obtain a monomer, polymer or polymer product. Process according to any one of embodiments 1 to 60 and / or 65 to 66, wherein the polymer or polymer product is a granulate, strand, rod, plate, pipe, foil, layer, film, sheet, fiber, filament, coating, extruded and / or molded article, soft foam, half-rigid foam and / or rigid foam. Process according to any one of embodiments 1 to 60 and / or 65 to 67, wherein the monomer is a di- or polyol; preferably butandiol; aldehyde; preferably formaldehyde; di- or polyisocyanate; preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (IPDI); amide; preferably caprolactam; alkene; preferably styrene, ethene and norbornene; alkyne, (di)ester; preferably methyl methacrylate; mono or diacid; preferably adipic acid or terephthalic acid; diamine; preferably hexamethylenediamine, nonanediamine, or sulfones; preferably 4,4'-dichlorodiphenyl sulfone. Process according to any one of embodiments 1 to 60 and / or 65 to 68, wherein the polymer is and / or the polymer product comprises polyamide (PA); preferably PA 6 and PA 66; polyisocyanate polyaddition product; preferably polyurethane (Pll), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (Teflon), thermoplastic polyurethanes (TPU), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis- 1 ,4-isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate coterephthalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PHA), poly-3- hydroxy butyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); and copolymers and mixtures thereof.

[0323] 70. Process according to any one of embodiments 1 to 60 and / or 65 to 69, wherein the polymer and / or the polymer product is / are or is / are a part of: a part of a car, preferably cylinder head cover, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing or housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part or part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, car exterior for A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, or cushion; a cloth, preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket; an electrical part, preferably electrical or electronic passive or active component, printed circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, connectors, microswitches, microbuttons, semiconductor, reflector housing for light-emitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hooks (snap-in) or spring tongue; a consumer and / or pharmaceutical product, preferably tennis string, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion or insulation; and / or packaging for the food industry; preferably mono- or multi-layer blown film, cast film (mono- or multi-layer), biaxially stretched film, laminating film.

[0324] 71 . Process according to any one of embodiments 1 to 60 and / or 65 to 70, wherein the content of the pyrolysis oil comprised in stream F0 in the purified pyrolysis oil, monomer, polymer and / or polymer product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the pyrolysis oil comprised in stream F0 in the purified pyrolysis oil, monomer, polymer and / or polymer product is 100 weight-% or less, preferably 95 weight- % or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.

[0325] 72. A purified pyrolysis oil, obtainable or obtained by a process according to any one of embodiments 1 to 60.

[0326] It is explicitly noted that the above set of embodiments represents a suitably structured part of the general description directed to preferred aspects of the present invention, and, thus, suitably supports, but does not represent the claims of the present invention.

[0327] In the context of the present invention, a term “X is one or more of A, B and C”, wherein X is a given feature and each of A, B and C stands for specific realization of said feature, is to be understood as disclosing that X is either A, or B, or C, or A and B, or A and C, or B and C, or A and B and C. In this regard, it is noted that the skilled person is capable of transfer to above abstract term to a concrete example, e.g. where X is a chemical element and A, B and C are concrete elements such as Li, Na, and K, or X is a temperature and A, B and C are concrete temperatures such as 10 °C, 20 °C, and 30 °C. In this regard, it is further noted that the skilled person is capable of extending the above term to less specific realizations of said feature, e.g. “X is one or more of A and B” disclosing that X is either A, or B, or A and B, or to more specific realizations of said feature, e.g. “X is one or more of A, B, C and D”, disclosing that X is either A, or B, or C, or D, or A and B, or A and C, or A and D, or B and C, or B and D, or C and D, or A and B and C, or A and B and D, or B and C and D, or A and B and C and D.

[0328] The converting steps to obtain the monomer, polymer or polymer product may comprise one or more synthesis steps and can be performed by conventional synthesis and technics well known to a person skilled in the art. Independent of the person skilled in the art to assess novelty and inventive step of the independent claims, the person skilled in the art to perform the converting step is from the technical field(s) pyrolysis, gasification, remonomerization, depolymerization and / or synthesis and / or production of monomers, polymers and polymer compounds, and its further processing (e.g. extrusion, injection molding). Examples of the steps of the conversion are described in “Industrial Organic Chemistry”, 3. volume, Wiley-VCH, 1997; ISBN: 978-3-527- 28838-0; „Kunststoffhandbuch“, 11 volumes in 17 sub-volumes, Carl Hanser Verlag, especially volume 6, „Polyamide“, 1. edition, 1966; volume 7, ..Polyurethane", 3. edition, 1993; and volume 8, “Polyester”, 1. edition 1973, “Industrial Organic Chemistry”, 3. volume, Wiley-VCH, 1997; ISBN: 978-3-527-28838-0, “Injection Molding Reference Guide, 4th edition, CreateSpace Independent Publishing Platform, 2011 , ISBN: 978-1466407824, EP0989146 (A1), EP1460094 (A1), W02006034800 (A1), EP1529792 (A1), W02006042674 (A1), EP0364854 (A2), US5506275 (A), EP0897402 (A1), WO2015082316 (A1), WO2021021855 (A1), WO2021126938 (A1), W02021021902 (A1), W02021092311 (A1), WO2008155271 (A1), WO2013139827 (A1), each of which is incorporated herein by reference.

[0329] The present invention is further illustrated by the following Examples.

[0330] Examples

[0331] Reference Example 1 Determination of the total acid number (TAN)

[0332] The total acid number was determined by titration with KOH according to ASTM D3242.

[0333] Reference Example 2 Measurement of N content (wppm)

[0334] The nitrogen content is determined by combustion of the respective sample at 1000°C. NO contained in resulting combustion gases reacts with ozone so that NO2* is formed. Relaxation of excited nitrogen species is detected by chemiluminescence detectors according to ASTM D4629 (N). Calibration range is from 0.5 wppm to 50 wppm. Samples with higher concentrations are diluted with xylene to be in calibration range.

[0335] Reference Example 3.1 Measurement of total chlorine content (wppm)

[0336] The sample is filtered with a 0.45|jm syringe filter before analysis. The chlorine content is determined by combustion of the respective sample at 1050°C. Resulting combustion gases, i.e., hydrogen chloride, are led into a cell in which coulometric titration is performed.

[0337] Reference Example 3.2 Measurement of chloride content (wppm) The sample is filtered with a 0.45|jm syringe filter before analysis. The chloride content is determined by ion chromatography. Apparatus: Ion chromatograph 850 Professional (Metrohm) (Pre column: Metrosep A Supp4 / 5 S-Guard and Analytical column: Metrosep A Supp 5 250 / 4; Flow: 0.7 mL / min; Column temperature: 30°C; Detector temperature: 40°C; Inject volume: 25 pL; Suppressor MSM HC Rotor A). As Eluant: 3.2 mmol / L Na2COs ; 1.0 mmol / L NaHCO3 and as Suppressor regenerant: 50 mmol / L sulfuric acid were used.

[0338] Sample preparation: 0.2 g - 0.4 g of the sample were weighed and dissolved in 10 mL toluene. For analyte extraction, 10 mL deionized water were added. After centrifugation, the aqueous phase was extracted and analyzed. Samples with a concentration below the limit value of the method were spiked with 20 pg / L chloride standard solution (corresponding to a limit value of 1 mg / kg chloride in the sample) to check the recovery rate.

[0339] Reference Example 4 Measurement of the total amount of the one or more organic compounds comprising conjugated double bonds

[0340] The diene content is determined by UOP326-17. In this procedure dienes are reacted with maleic anhydride (MA) and the consumption of MA is determined (by titration of the remainder MA). It can be expressed as g(l2) / 100g(sample) or alternatively as g(MA) / 100g(sample). The unit can be interconverted by multiplying the MA-value (MAV) by a factor 2.59 to obtain the value expressed with g(l2) / 100g(sample) corresponding to the molar weight of I2 and MA. Accordingly, 1wt% Styrene or 0.52 wt.-% Butadiene correspond to 0.94g(MA) / 100g or 2.43g(l2) / 100g.

[0341] Reference Example 5 Measurement of oxygen content

[0342] O-content is determined by ASTM D5622.The sample is pyrolyzed in a reductive gas atmosphere on a soot contact, the oxygen is converted hereby to carbon monoxide (CO). The carbon monoxide is detected and quantified via IR spectrometry.

[0343] Reference Example 6 Measurement of S content (wppm)

[0344] The sulfur content is determined by combustion of the respective sample at 1000°C. Sulfur dioxide which is contained in resulting combustion gases is excited by UV (ultraviolet) light. Light which is emitted during relaxation is detected by UV fluorescence detectors according to ASTM D5453 (S). Calibration range is from 0.5 wppm to 50 wppm. Samples with higher concentrations are diluted with xylene to be in calibration range.

[0345] Reference Example 7 Determination of the styrene content GC method with a nonpolar, 100% dimethylpolysiloxane phase column and FID-detector. Final column temperature and inlet temperature are 330°C and 320°C, respectively. Integrated area signal of Styrene as ratio of all integrated peaks times 100% is Area%. Area% roughly correlates with wt.%.

[0346] Reference Example 8 Reactor loading and test setup

[0347] All reaction steps of the examples, except for the extraction, were conducted in reactors with inner diameter of 10mm and were operated in trickle bed mode (downflow). The reactor (80cm in length) is loaded with corundum (WSK F46; commercial corundum) from the bottom such that the lower 25 cm are filled with inert corundum (cooling zone). On top of this the 30cm long adsorbents bed is placed from 25 to 55 cm and in this zone the reaction temperature is maintained. In case no catalyst nor adsorbent is used this zone is filled with corundum only (WSK F46; commercial corundum). On top of the catalyst resp. adsorbents bed corundum (WSK F46; commercial corundum) is filled from 55 to 80cm. In this corundum zone the feed is preheated to the reaction temperature whereas in the lower corundum filled zone the product stream is cooled from the reactor temperature down to the trace heating temperature.

[0348] Example 1 Process for purifying a pyrolysis oil according to the present invention

[0349] A feed stream F0 comprising a pyrolysis oil having a total acid number (TAN) of 20.4 mg(KOH) / g(feed), a total chlorine content of 590 wppm, a chloride content of 1 wppm, a nitrogen content of about 3260 wppm, an oxygen content of about 0.82 g(0) / 100g(feed), and a density of 0.8653 g / ml was subjected to an extraction with NaOH, in particular F0 (5 L of pyrolysis oil) were introduced in a stirred 12L steel container and mixed with 1 ,5L of demin. water. Next a feed stream FN comprising 0.3M NaOH solution (3.5 L of 0.3M NaOH solution) were pumped for a time period of 50 minutes into the mixing device (12L steel container) while stirring was occurring. Once 3.5 L of the NaOH solution (FN) was added, the obtained mixture was further stirred for 30 minutes. The mixing was then stopped such that the two-phase mixture could settle overnight in the mixing device. The pH of the aqueous mixture was measured and of about 8. The overall procedure, namely mixing and settling, was performed at 40 °C for dissolving contained waxes. The oil phase was separated from the aqueous phase (Fw), the aqueous phase was removed from the mixing / settling device to waste water treatment and the oil phase (stream F1) was removed from the mixing / settling device for subsequent dechlorination. The obtained oil phase (stream F1) comprising the pyrolysis oil with a reduced total acid number (TAN) of about 4 mg(KOH) / g(feed), the N-content, the O-content and the Cl-content was not changed significantly compared to F0. The stream F1 was then subjected to dechlorination in a reactor comprising a Cl-adsorbent (hydrotalcite: aluminum-magnesium hydroxycarbonate powder having a MgOAhCh weight ratio of 70:30) in the presence of H2 at 350 °C and at a pressure of 50 bar. Before use, the adsorbent was compacted, then crushed and sieved to an average particle size of 500-1000 micrometers. Further, it was calcined at 450°C for 5h in air and equilibrated in ambient air overnight. Prior to entering F1 in the reactor, the obtained Cl-adsorbent was dried at 100°C and 200°C at a gas hourly space velocity (GHSV) =2000 / h in nitrogen under ambient pressure for 1 hour each while ramping temperature with 1 K / min. At 200°C, gas was switched from N2 to H2 and the pressure was increased to 50 bar within 1 hour. After the pressure was attained, the GHSV was reduced to 475 / h and the reactor was heated to 350°C with 1 K / min. Once 350 °C were attained, S1 was introduced in the reactor at a liquid hourly space velocity (LHSV) =0.95 / h. The resultant product stream was analyzed as shown in Table 2.1 and had a reduced total chlorine content (at the beginning of the operation reduced by about 90 %).

[0350] Table 1 Chlorine and chloride contents for F1 and product stream from dechlorination at various time on stream (TOS)

[0351] The intermediate products (F2) within the course of the reaction were combined to form the feed F2. The resultant feed stream F2 had in average a total chlorine content of 260 wppm and a chloride content of 1 wppm. The N-, O-contents were not changed compared to F1.

[0352] Comparative Example 1 Process for purifying a pyrolysis oil not according to the present invention

[0353] As opposed to Example 1 , the process was started with a dechlorination step, there was no extraction. A feed stream F0 comprising a pyrolysis oil as the one in Example 1 , namely having a total acid number (TAN) of about 20 mg(KOH) / g(feed), a total chlorine content of 560 wppm, a chloride content of 1 wppm, a nitrogen content of about 3260 wppm, an oxygen content of about 0.82 g(0) / 100g(feed), and a density of 0.8653 g / ml, was subjected to dechlorination in a reactor comprising a Cl-adsorbent (hydrotalcite: aluminum-magnesium hydroxycarbonate powder having a MgOAhCh weight ratio of 70:30) in the presence of H2 at 350 °C and at a pressure of 50 bar. Before use, the adsorbent was compacted, then crushed and sieved to an average particle size of 500-1000 micrometers. Further, it was calcined at 450°C for 5h in air and equilibrated in ambient air overnight. Prior to entering F0 in the reactor, the obtained Cl-adsorbent was dried at 100°C and 200°C at a gas hourly space velocity (GHSV) =2000 / h in nitrogen under ambient pressure for 1 hour each while ramping temperature with 1 K / min. At 200°C, gas was switched from N2 to H2 and the pressure was increased to 50 bar within 1 hour. After the pressure was attained, the GHSV was reduced to 475 / h and the reactor was heated to 350°C with 1 K / min. Once 350 °C were attained, F0 was introduced in the reactor at a liquid hourly space velocity (LHSV) =0.95 / h.

[0354] After 12.5 h TOS, the pressure drop in the reactor system increased above 10 bar so that the feed dosing had to be stopped and the reactor was cooled down, purged with toluene and dried with nitrogen. The pressure drop of the reactor is externally determined with 100mln(N2) / min at ambient outlet pressure resulting in 535 mbar whereas the reactor's pressure drop before testing was determined with 28 mbar. The test period was too short so that before the first planed sampling after 30h the test rig was run down due to too high pressure.

[0355] Table 2 Comparison pressure drop / TAN after dechlorination alone or after extraction + dechlorination

[0356] Reference Example 9: Extraction - step (ii) according to the present invention

[0357] A feed stream F0 comprising a pyrolysis oil having a total acid number (TAN) of about 8.5 mg KOH / g, a total chlorine content of 24 wppm, a chloride content < 5 wppm, a nitrogen content of 0.5 wt.-% based on the weight of the pyrolysis oil and an oxygen content of 1 wt.-% based on the weight of the pyrolysis oil, a density of 916 kg / m3and a viscosity of 6.4 mPas, was subjected to extraction with KOH at pH 7 at T = 50°C. To do so, FO was introduced in a 1.3 L agitated glass vessel. Demineralized water was then added into the vessel (phase ratio v (water / pyrolysis oil) = 0.5 kg / kg) forming a mixture. The pH of the aqueous phase of the mixture was adjusted to 7.2 with 25 wt.-% KOH. The obtained mixture was mixed for 15 min. The obtained aqueous phase was separated after settling (for 2 minutes) from the organic phase. The organic phase was analyzed.

[0358] Again, a washing step was done. Demineralized water was added to the organic phase with a phase ratio v (demineralized water / organic phase) = 0.5 kg / kg to remove salts and caustic entrainment from the pyrolysis oil. The results are listed in Table 5 below.

[0359] Table 3

[0360] *pH of the aqueous phase

[0361] **pH of the aqueous phase of FO after FO was simply washed with demineralized water.

[0362] As may be taken from Table 3, at pH 7 and with KOH, the TAN, O and N content could be reduced. Thus, such type extraction (conditions, etc.) could also be used prior to dechlorination as in Example 1. Indeed, this will permit to avoid fouling of the production unit, increase the TOS and reduce pressure drop as demonstrated by the comparison of Example 1 with Comparative Example 1.

[0363] Example 2 Testing of extracted pyrolysis oils obtained according to step (ii)

[0364] In this example, extracted pyrolysis oils obtained according to (ii) of the present invention, namely by performing an extraction as described in Example 1, have been subjected to thermal treatment only and compared to non-extracted pyrolysis oils.

[0365] A feed stream F1 (extracted pyrolysis oil) having a TAN of about 4 mg(KOH) / g(feed)), a nitrogen content of about 3260 wppm, an oxygen content of about 0.82 g(O) / 100g (feed), a MAV of 9.01 g(l2) / 100g , a styrene content of 6.1 Area% determined by GC, a total chlorine content of 560 wppm, a chloride content of 1 wppm, and a density of 0.8653 g / ml is obtained and compared to a feed stream F11 (non-extracted pyrolysis oil) having a TAN of about 20 mg(KOH) / g(feed)), a nitrogen content of about 3260 wppm, an oxygen content of about 0.82 g(O) / 100g (feed), a MAV of 9.01 g(l2) / 100g , a styrene content of 6.1 Area% determined by GC, a total chlorine content of 560 wppm, a chloride content of 1 wppm, and a density of 0.8653 g / ml.

[0366] F1 and F11 were subjected separately to different thermal treatments. The Feeds were dosed into a reactor filled with inert (corundum as indicated in Ref. example 8) with a dosing rate of 20ml / h corresponding to a LHSV=0.85 / h if the inert volume in the reaction zone is taken as reactive volume. Pressure and temperature were varied equally in both experiments and samples taken close to the end of each condition. The degree of polymerization of styrene has been determined under different conditions and compared for each sample. Degree of polymerization is calculated from the Area%-values of the feed and the samples taken during the experiments. Complete loss of styrene equals 100% degree of polymerization of styrene. Table 4

[0367] Extracted feed (F1)

[0368] Table 5

[0369] Not extracted feed (F11)

[0370] Thus, this example demonstrates that performing extraction before a subsequent thermal treatment permits not only to reduce the total acid number (TAN) of the obtained pyrolysis oil but also clearly reduces the formation of solids, in particular due to the polymerization of styrene - which is clearly reduced as may be taken from Tables 4 and 5 above. This permits to better enable subsequent pyrolysis oil purification and / or subsequent heat-up steps (lower pressure drop, longer TOS expected). Without wanting to be bound by any theory, this examples shows that extracting the pyrolysis oil prior to a subsequent thermal treatment according to the process of the present invention prevents further polymerization of styrene monomers comprised in the pyrolysis oil and thus reduces the amount of impurities of the pyrolysis oil which hinder further purification of the pyrolysis oil.

[0371] Reference Example 10 Particle size (D50)

[0372] The D50 particle size was determined by optical methods or by an air sieve, for example by various instruments, namely, Cilas Granulometer 1064 supplied by Quantachrome, Malvern Mastersizer or Luftstrahlsieb (air sieve) supplied by Alpine.

[0373] Reference Example 11 Determination of the average pore volume

[0374] Pore volume can be derived from BET measurements (for micro and mesopores) or alternatively Hg porosimetry (for macropores). The Determination of Pore Volume and Area Distributions in Porous Substances. I. Computations from Nitrogen Isotherms JACS 1951 (73) 373-380 E.P. Barret, L.G. Joyner, P.P. Halenda.

[0375] Reference Example 12 Determination of the BET specific surface area

[0376] The BET surface area of the adsorbent material is measured by using an instrument supplied by Quantachrome (Nova series) or by Micromeritics (Gemini series). The method entails low temperature adsorption of nitrogen at the BET region of the adsorption isotherm.

[0377] Comparative Example 2 Process for purifying a pyrolysis oil not according to the present invention

[0378] A feed stream F0 comprising a pyrolysis oil having a total acid number (TAN) of 7 mg KOH / g was subjected to a first washing step with demineralized water into a 250 ml glass bottle with a phase ratio of v (demin. water / pyrolysis oil (F0)) = 1 kg / kg. The mixture was shook. The pH of the aqueous phase of the mixture was of pH 4.3. The obtained mixture water / organic phase (oil) was introduced into a centrifuge. The aqueous phase was thus separated from the organic (oil) phase.

[0379] After separating of the water phase from the organic phase, demineralized water was further added to the organic phase for a second washing step. Demineralized water was added with a phase ratio v (demineralized water / organic phase) = 1kg / kg. The obtained mixture water / or- ganic phase (oil) was introduced into a centrifuge. The aqueous phase was separated after from the organic phase. Finally, a third washing step was performed and the aqueous phase was separated with a centrifuge from the organic phase, said washed organic phase was analyzed. The results are listed in Table 3 below.

[0380] Table 6

[0381] *pH of the aqueous phase

[0382] **pH of the aqueous phase of FO after FO was simply washed with demineralized water. As may be taken from Table 6, washing steps are not sufficient for reducing the TAN number.

[0383] Reference Example 13: Testing of different bases

[0384] In this example, pyrolysis oils (each of them having a total acid number (TAN) of about 8.5 mg KOH / g, a total chlorine content of 24 wppm, a chloride content < 5 wppm, a nitrogen content of 0.5 wt.-% based on the weight of the pyrolysis oil and an oxygen content of 1 wt.-% based on the weight of the pyrolysis oil, a density of 916 kg / m3and a viscosity of 6.4 mPas) have been extracted with NaOH or KOH in centrifuge glasses under the conditions detailed in Table 9. After the extraction, phase separation of these oils have been observed (cf. Table 9).

[0385] Table 9

[0386] As may be taken from Table 9, using NaOH for the extraction of pyrolysis oil at a pH of about 10 lead to the formation of a solid such that no phase separation was visible in gravity field between the aqueous and the oil phase. A further centrifugation step was required to separate the Solid, the aqueous and the oil phase after extraction. When the pH during extraction was reduced, less solid formed and the phase separation between the aqueous and the oil phase was clearly visible - thus making it easy to separate the aqueous and the oil phase after extraction. Further, less solid formed at a pH of about 10 when using KOH for the extraction of pyrolysis oil. Without wanting to be bound by any theory, using NaOH for the extraction of pyrolysis oil may lead to the formation of sodium soaps (sodium salts of fatty acids) which are mostly solid and which thus hinder the phase separation of the aqueous and the oil phase after extraction, in contrast to potassium soaps (potassium salt of fatty acids) which are mostly liquid and thus do not hinder the phase separation of the aqueous and the oil phase after extraction. Therefore, KOH might be selected over NaOH to avoid these drawbacks.

[0387] Cited literature

[0388] - WO 2017 / 083018 A1

[0389] - WO 2020 / 178597 A 1

[0390] - WO 2014 / 165859 A1

Claims

Claims1 . A process for purifying a pyrolysis oil, the process comprising:(i) providing a stream F0 comprising a pyrolysis oil, the pyrolysis oil comprising one or more halogenated organic compounds and one or more organic compounds comprising conjugated double bonds;(ii) subjecting the stream F0 provided in (i) to extraction in at least one extraction zone ZE, obtaining a stream F1 comprising the extracted pyrolysis oil, wherein (ii) comprises:(ii.1 ) introducing F0 into ZE;(11.2) bringing in contact F0 with water and a base B into ZE at a temperature in the range of from 10 to 200 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 ;(11.3) separating PA from Po, obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil;(iii) subjecting the stream F1 obtained according to (ii) to thermal treatment in at least one thermal treating zone ZP, ZP being located downstream of ZE, obtaining a stream F2 being depleted, compared to F1 , in one or more of the one or more organic compounds comprising conjugated double bonds and the one or more halogenated organic compounds.

2. The process of claim 1 , wherein no organic solvent is used in the extraction according to (ii).

3. The process of claim 1 or 2, wherein the extraction according to (ii) is performed at a temperature in the range of from 10 to 95 °C, preferably in the range of from 15 to 90°C, more preferably in the range of from 20 to 85 °C, more preferably in the range of from 25 to 80 °C; wherein the extraction according to (ii) is preferably performed at a pressure PE in the range of from 0.8 to 1.2 bar(abs), more preferably in the range of from 0.9 to 1.1 bar(abs).

4. The process of any one of claims 1 to 3, wherein the base B is one or more of an alkali metal compound, an alkaline earth metal compound and ammonia, preferably B is an alkali metal compound being one or more of potassium hydroxide, sodium hydroxide, potassium carbonate, sodium carbonate, potassium bicarbonate and sodium bicarbonate, more preferably one or more of potassium hydroxide, sodium hydroxide, potassium carbonate and sodium carbonate, more preferably one or more of potassium hydroxide and sodiumhydroxide, more preferably potassium hydroxide or sodium hydroxide, more preferably potassium hydroxide.

5. The process of any one of claims 1 to 4, wherein for the extraction according to (ii), the weight ratio of water to F0 in ZE is in the range of from 0.05:1 to 2:1 , preferably in the range of from 0.1 :1 to 1.5:1 , more preferably in the range of from 0.1 :1 to 1.2:1 , more preferably in the range of from 0.1 :1 to 0.7:1 , more preferably in the range of from 0.2:1 to 0.5:1 , more preferably in the range of from 0.3:1 to 0.5:1.

6. The process of any one of claims 1 to 5, wherein (ii.2) comprises(11.2.1) introducing water and B, preferably a mixture of water and B, into ZE;(11.2.2) bringing in contact, preferably mixing, F0 with water and B, preferably the mixture of water and B, into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , preferably in the range of from 7 to 10; or wherein (ii.2) comprises(ii.2.1’) introducing water into ZE;(ii.2.2’) bringing in contact, preferably mixing, F0 with water into ZE, obtaining a mixture comprising water and the pyrolysis oil;(ii.2.3’) introducing B into ZE and bringing in contact, preferably mixing, B with the mixture obtained in (ii.2.2’) into ZE, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 , preferably in the range of from 7 to 10.

7. The process of any one of claims 1 to 6, wherein (ii) comprises(11.1) introducing F0 into a mixing unit UM1 comprised in ZE;(11.2) mixing F0 with water and a base B into UM1 at a temperature in the range of from 10 to 200 °C, preferably from 10 to 95 °C, obtaining a mixture M comprising an aqueous phase PA and an organic phase Po, the pH of the aqueous phase PA of M being in the range of from 7 to 11 ; removing M from UM1 ;(11.3) separating PA from Po, wherein (ii.3) comprises(ii.3.1) passing M into a liquid-liquid separation unit US1 comprised in ZE, US1 being located downstream of UM1 , obtaining a stream FA comprising PA and a stream F1 comprising Po being the extracted pyrolysis oil; removing F1 from ZE;wherein preferably separating PA from Po according to (ii.3) is performed by decantation or centrifugation, more preferably decantation.

8. The process of any one of claims 1 to 7, wherein the thermal treatment according to (iii) is one or more of dehalogenation, hydrogenation, hydroprocessing, heat-up for dehalogenation, heat-up for hydrogenation, heat-up for hydroprocessing and distillation.

9. The process of any one of claims 1 to 8, wherein (iii) comprises(111.1) optionally subjecting the stream F1 obtained according to (ii) to hydrogenation in at least one reaction zone ZH containing a heterogeneous hydrogenation catalyst, ZH being comprised in ZP, obtaining a stream FH being depleted, compared to F1 , in the one or more organic compounds comprising conjugated double bonds;(111.2) subjecting the stream F1 obtained according to (ii), or FH obtained according to (iii.1 ), to dehalogenation in at least one dehalogenation zone ZD comprised in ZP, and located downstream of ZH if present, obtaining a stream F2 being depleted, compared to F1 , or FH when (iii.1) is performed, in the one or more halogenated organic compounds.

10. The process of claim 9, wherein the dehalogenation zone ZD according to (iii.2) comprises, preferably is an adsorption zone, preferably comprising a heterogeneous adsorbent material suitable for adsorbing halide comprised in at least one of the one or more halogenated organic compounds, preferably in all of the one or more halogenated organic compounds.11 . The process of any one of claim 9 or 10, wherein (iii.2) comprises(111.2.1) introducing a gas stream G1 into ZD, preferably being an adsorption zone, preferably a gas stream G1 comprising one or more of hydrogen and nitrogen, more preferably hydrogen;(111.2.2) introducing the stream F1 obtained from (ii), or FH obtained in (iii.1), into ZD;(111.2.3) bringing F1 , or FH, in contact with G1 and optionally a heterogeneous adsorbent material comprised in ZD, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds;(111.2.4) removing F2 from ZD.

12. The process of claim 11 , wherein the gas stream G1 has a temperature in the range of 150 to 500°C, preferably in the range of from 300 to 400 °C;wherein preferably the gas stream G1 is introduced at a pressure in the range of from 1 to 100 bar(abs), more preferably in the range of from 5 to 80 bar(abs), more preferably in the range of from 10 to 50 bar(abs).

13. The process of claim 9, wherein dehalogenation according to (iii.2) comprises(iii.2.1 ’) optionally introducing a gas stream G11 into ZD, being a reactor which is free of any adsorbent material and free of any catalyst, preferably the gas stream G11 comprising one or more of hydrogen and nitrogen, more preferably hydrogen;(iii.2.2’) introducing the stream F1 obtained from (ii), or FH obtained in (iii.1), into ZD;(iii.2.3’) heating F1 , or FH, into the reactor to a temperature in the range of from 80 to400 °C, preferably in the range of from 200 to 400 °C, and bringing in contact F1 , or FH, with G11 , if (iii.

2. T) is performed, obtaining a stream F2 being depleted, compared to F1 , or FH, in the one or more halogenated organic compounds;(iii.2.4’) removing F2 from ZD.

14. The process of any one of claims 1 to 8, wherein (iii) comprises(iii.T) subjecting the stream F1 obtained according to (ii) to distillation in at least one distillation zone ZL, ZL being comprised in ZP, obtaining a stream F2 being depleted, compared to F1 , in the one or more organic compounds and a stream F3 being enriched compared to F1 , in the one or more organic compounds.

15. The process of any one of claims 1 to 14, further comprising, after (iii), one or more of a steam cracking step, a hydrocracking step, a hydroprocessing step, a distillation step, a stripping step, a storage step, and an aqueous extraction step.

16. A production unit for carrying out the process for purifying a pyrolysis oil according to any one of claims 1 to 15, the unit comprising an inlet means for introducing F0 into ZE; an outlet means for removing F1 from ZE; at least one extraction zone ZE, at least one thermal treating zone ZP, ZP being located downstream of ZE; an inlet means for introducing F1 into ZP; an outlet means for removing F2 from ZD.

17. Process comprising the step:using the production unit according to claim 16 to obtain a purified pyrolysis oil, monomer, polymer or polymer product.

18. Process, preferably comprising the steps according to any one of claims 1 to 15, comprising the further step: converting the stream F2 obtainable or obtained by the process according to any one of claims 1 to 14 or a chemical material obtainable by or obtained by the process according to claim 15 to obtain a monomer, polymer or polymer product.

19. Process according to claim 17 or 18, wherein the polymer or polymer product is a granulate, strand, rod, plate, pipe, foil, layer, film, sheet, fiber, filament, coating, extruded and / or molded article, soft foam, half-rigid foam and / or rigid foam.

20. Process according to any one of claims 17 to 19, wherein the monomer is a di- or polyol; preferably butandiol; aldehyde; preferably formaldehyde; di- or polyisocyanate; preferably methylene diphenyl diisocyanate (MDI), polymeric methylene diphenyl diisocyanate (pMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI) or isophoronediisocyanate (I PDI); amide; preferably caprolactam; alkene; preferably styrene, ethene and norbornene; alkyne, (di)ester; preferably methyl methacrylate; mono or diacid; preferably adipic acid or terephthalic acid; diamine; preferably hexamethylenediamine, nonanediamine, or sulfones; preferably 4,4'-dichlorodiphenyl sulfone.

21. Process according to any one of claims 17 to 20, wherein the polymer is and / or the polymer product comprises polyamide (PA); preferably PA 6 and PA 66; polyisocyanate polyaddition product; preferably polyurethane (Pll), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), poly acrylonitrile butadiene styrene (ABS), poly styrene acrylonitrile (SAN), poly acrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (Teflon), thermoplastic polyurethanes (TPU), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis- 1 ,4-isoprene), poly(trans-1 ,4-isoprene), polyoxymethylene (POM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate coterephthalate (PBAT), polyester (PES), polyether sulfone (PESU), polyhydroxyalkanoate (PHA), poly-3- hydroxy butyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), pol-yhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSLI), polycarbonate (PC), polyether ether ketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); and copolymers and mixtures thereof.

22. Process according to any one of claims 17 to 21 , wherein the polymer and / or the polymer product is / are or is / are a part of: a part of a car, preferably cylinder head cover, engine cover, housing for charge air cooler, charge air cooler flap, intake pipe, intake manifold, connector, gear wheel, fan wheel, cooling water box, housing or housing part for heat exchanger, coolant cooler, charge air cooler, thermostat, water pump, radiator, fastening part or part of battery system for electromobility, dashboard, steering column switch, seat, headrest, center console, transmission component, door module, car exterior for A, B, C or D pillar cover, spoiler, door handle, exterior mirror, windscreen wiper, windscreen wiper protection housing, decorative grill, cover strip, roof rail, window frame, sunroof frame, antenna panel, headlight and taillight, engine cover, cylinder head cover, intake manifold, airbag, or cushion; a cloth, preferably shirt, trousers, pullover, boot, shoe, shoe sole, tight or jacket; an electrical part, preferably electrical or electronic passive or active component, printed circuit board, printed circuit board, housing component, foil, line, switch, plug, socket, distributor, relay, resistor, capacitor, inductor, bobbin, lamp, diode, LED, transistor, connector, regulator, integrated circuit (IC), processor, controller, memory, sensor, connectors, microswitches, microbuttons, semiconductor, reflector housing for light-emitting diodes (LED), fastener for electrical or electronic component, spacer, bolt, strip, slide-in guide, screw, nut, film hinge, snap hooks (snap-in) or spring tongue; a consumer and / or pharmaceutical product, preferably tennis string, climbing rope, bristle, brush, artificial grass, 3D printing filament, grass trimmer, zipper, hook and loop fastener, paper machine clothing, extrusion coating, fishing line, fishing net, offshore line and rope, vial, syringe, ampoule, bottle, sliding element, spindle nut, chain conveyor, plain bearing, roller, wheel, gear, roller, ring gear, screw and spring dampers, hose, pipeline, cable sheathing, socket, switch, cable tie, fan wheel, carpet, box or bottle for cosmetics, mattress, cushion or insulation; and / or packaging for the food industry; preferably mono- or multi-layer blown film, cast film (mono- or multi-layer), biaxially stretched film, laminating film.

23. Process according to any one of claims 17 to 22,wherein the content of the pyrolysis oil comprised in stream FO in the purified pyrolysis oil, monomer, polymer and / or polymer product is 1 weight-% or more, preferably 2 weight-% or more, more preferably 5 weight-% or more, more preferably 15 weight-% or more, more preferably 30 weight-% or more, more preferably 40 weight-% or more, more preferably 60 weight-% or more, more preferably 80 weight-% or more, more preferably 90 weight-% or more, more preferably 95 weight-% or more; and / or wherein the content of the pyrolysis oil comprised in stream F0 in the purified pyrolysis oil, monomer, polymer and / or polymer product is 100 weight-% or less, preferably 95 weight- % or less, more preferably 90 weight-% or less, more preferably 50 weight-% or less, more preferably 25 weight-% or less, more preferably 10 weight-% or less; and preferably wherein the content is determined based on identity preservation and / or segregation and / or mass balance and / or book and claim chain of custody models, preferably based on mass balance, preferably the International Sustainability and Carbon Certification (ISCC) standard.

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