Process for refining pyrolysis oil

Abstract

The present invention relates to a process for refining pyrolysis oil and a unit for carrying out the process. The present invention further relates to refined pyrolysis oil that can be obtained or obtained by the process.

Description

[Technical Field]

[0001] The present invention relates to a process for refining pyrolysis oil and a unit for carrying out the process. The present invention further relates to refined pyrolysis oil that can be obtained or obtained by the process. [Background technology]

[0002] Currently, the majority of plastic waste is still landfilled or incinerated to generate heat. Chemical recycling is an attractive method of converting waste plastic materials and tires into useful chemicals. A key technique for chemically recycling plastic waste or tires is pyrolysis. Pyrolysis is the thermal degradation of waste materials in an inert atmosphere, producing value-added products such as pyrolysis gases, liquid pyrolysis oils, and char (residue), with pyrolysis oil being the main product. Pyrolysis gases and chars can be used as fuels to generate heat, for example, for heating reactors. Pyrolysis oils can be used as raw materials for synthesis gas production and / or can be processed into chemical raw materials, such as ethylene, propylene, C4 cuts, etc., in (steam) crackers, for example.

[0003] Typically, plastic waste and tires are composed of different types of polymers. These polymers are often composed of carbon and hydrogen in combination with other elements, such as chlorine, bromine, fluorine, sulfur, oxygen, and nitrogen, which often complicate recycling efforts. If unrefined, the pyrolysis oils obtained from these materials can be damaged by corrosion, for example, during storage or decomposition. Therefore, high-quality pyrolysis oils are preferred as raw materials to prevent corrosion problems in downstream refinery processes.

[0004] U.S. Patent Application Publication No. 2021 / 0277324 discloses the purification of pyrolysis oil by treating the oil with sodium hydroxide at a temperature of 240°C. International Publication No. 2014 / 165859 discloses a method for purifying pyrolysis oil by reducing the content of contaminants, such as acids and metals. Furthermore, International Publication No. 2020 / 178599 discloses a process for upgrading pyrolysis oil, which includes washing the pyrolysis oil with water, then washing the pyrolysis oil with an alkane, and treating the resulting organic phase with an upgrading solution containing a polar organic solvent.

[0005] However, there remains a need to provide improved processes for refining pyrolysis oils obtained from waste materials, such as plastics and tires. In particular, there remains a need to provide improved processes that enable reduction of corrosion in downstream processes and / or storage. [Prior art documents] [Patent Documents]

[0006] [Patent Document 1] U.S. Patent Application Publication No. 2021 / 0277324 [Patent Document 2] International Publication No. 2014 / 165859 Pamphlet [Patent Document 3] International Publication No. 2020 / 178599 Brochure [Overview of the project] [Problems that the invention aims to solve]

[0007] Therefore, there is a need to provide a process for refining pyrolysis oil, preferably obtained from waste materials, particularly by reducing the total acid value and oxygen content. In fact, there is a need to provide high-value refined pyrolysis oil while using economical methods. [Means for solving the problem]

[0008] Thus, the present invention is a process for purifying pyrolysis oil, comprising: (i) providing a stream F0 containing pyrolysis oil; (ii) subjecting the stream F0 provided in (i) to extraction in at least one extraction zone Z to obtain a stream F1 containing the extracted pyrolysis oil, the step comprising: (ii.1) introducing F0 into an extraction unit UM1 provided in Z E ; (ii.2) contacting F0 with water and a base B in UM1 at a temperature T1 in the range of 10 to 200 °C to obtain a mixture M1 comprising an aqueous phase P A (1) and an organic phase P O (1), the step wherein the pH of the aqueous phase P A (1) in M1 is in the range of 7.5 to 11; (ii.3) passing the mixture M1 obtained according to (ii.2) through a liquid-liquid separation unit US1 provided in Z E and located downstream of UM1 to obtain a stream F A (1) containing P A and a stream F1 containing P O (1) which is the extracted pyrolysis oil; (ii.4) removing F1 from Z E ; and (iii) subjecting the stream F1 provided in (ii) to washing in at least one washing zone Z E located downstream of Z W to obtain a stream F2 containing purified pyrolysis oil; and relates to a process.

Brief Description of the Drawings

[0009] [Figure 1]Schematic diagram of a unit for implementing a process for purifying pyrolysis oil according to an embodiment of the present invention. The unit comprises an extraction unit UM1 and a liquid-liquid separation unit US1, an extraction zone ZE in which US1 is located downstream of UM1, and a washing zone ZW downstream of ZE, which comprises a washing unit UM2 and a liquid-liquid separation unit US2, in which US2 is located downstream of UM2. A stream F0 containing pyrolysis oil is introduced into UM1 together with water and a base B. F0, water and B are contacted in UM1 at a temperature in the range from 10 to 200 °C, preferably in the range from 10 to 95 °C. A mixture M1 is removed from UM1, the mixture comprising an aqueous phase PA(1) and an organic phase PO(1), the pH of the aqueous phase PA(1) of M1 being in the range from 7.5 to 11. M1 is introduced into US1. A stream FA(1) containing PA(1) and a stream F1 containing the extracted pyrolysis oil (PO(1)) are obtained and removed from US1 and ZE. Furthermore, F1 is introduced into UM2 together with water. F1 and water are contacted at a temperature in the range from 10 to 95 °C. A mixture M2 is obtained, the 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 from 7.5 to 11 and the pH of PA(2) < the pH of PA(1). Then, M2 is introduced into US2. A stream F2 containing purified pyrolysis oil is obtained. A further stream FA(2) containing PA(2) is also obtained. Then, F2 can be stored or transferred for further processing. Optionally, the aqueous stream, which is FA(1), and / or the aqueous stream, which is FA(2), are recycled (not shown) in UM1 and / or UM2. Optionally, if a precipitate is formed at the interface between PA(1) and PO(1), the precipitate is removed from US1 by purge (not shown). [Figure 2]This is a schematic diagram of a unit for carrying out a process for purifying pyrolysis oil according to an embodiment of the present invention. The unit comprises an extraction unit UM1, a solid-liquid separation unit SLS1, and a liquid-liquid separation unit US1, with SLS1 located downstream of UM1 and US1 located downstream of SLS1 in an extraction zone ZE, and a washing zone ZW located downstream of ZE, with a washing unit UM2, a solid-liquid separation unit SLS2, and a liquid-liquid separation unit US2, with SLS2 located downstream of UM2 and US2 located downstream of SLS2. The process is as defined in Figure 1, except that M1 passes through SLS1 before being introduced into US1 to remove any solids present, and M2 passes through SLS2 before being introduced into US2 to remove any solids present. [Figure 3]Schematic diagram of a unit for implementing a process for purifying pyrolysis oil according to an embodiment of the present invention. The unit comprises an extraction unit UM1 and a liquid-liquid separation unit US1, and US1 comprises an extraction zone ZE located downstream of UM1 and a washing zone ZW downstream of ZE and comprising a washing unit UM2 combined with a liquid-liquid separation unit US2. ZE optionally comprises a solid-liquid separation unit SLS1 located downstream of UM1 and upstream of US1. A stream F0 containing pyrolysis oil is introduced into UM1 together with water and a base B. F0, water and B are brought into contact in UM1 at a temperature in the range from 10 to 200 °C, preferably in the range from 10 to 95 °C. A mixture M1 is removed from UM1, said mixture comprising an aqueous phase PA(1) and an organic phase PO(1), and the pH of the aqueous phase PA(1) of M1 is in the range from 7.5 to 11. M1 is introduced into US1. When SLS1 is present, M1 passes through SLS1 before being introduced into US1. A stream FA(1) containing PA(1) and a stream F1 containing extracted pyrolysis oil are obtained and removed from US1 and ZE. Furthermore, F1 is introduced into a combined UM2 / US2 which is an extraction column. Water is also introduced into said column and brought into contact with F1 at a temperature in the range from 10 to 95 °C, the phases of M2 are separated within the column, the pH of the aqueous phase PA(2) of M2 is in the range from 7.5 to 11, and pH of PA(2) < pH of PA(1). A stream F2 containing purified pyrolysis oil is obtained (removed at the top of the column). A further stream FA(2) containing PA(2) is also obtained (removed on the opposite side of the column, i.e., at the bottom). Then F2 can be stored or transferred for further processing. Optionally, the aqueous stream, which is FA(2), is recycled in UM1 and / or ZW (not shown). [Figure 4]Schematic diagram of a unit for implementing a process for purifying pyrolysis oil according to an embodiment of the present invention. The unit comprises an extraction unit UM1, an optional solid-liquid separation unit SLS1 and a liquid-liquid separation unit US1, with SLS1 located downstream of UM1 and US1 located downstream of SLS1. An extraction zone ZE is provided downstream of US1, and a washing zone ZW is provided downstream of ZE, which comprises a washing unit UM2, an optional solid-liquid separation unit SLS2 and a liquid-liquid separation unit US2, with SLS2 located downstream of UM2 and US2 located downstream of SLS2. This process is as defined in Figure 1, except that M1 before being introduced into US1 optionally passes through SLS1 to remove solids if present, and M2 before being introduced into US2 optionally passes through SLS2 to remove solids if present. The ZW of the unit further comprises a washing unit UM4, an optional solid-liquid separation unit SLS4 and a liquid-liquid separation unit US4, with SLS4 located downstream of UM4 and US4 located downstream of SLS4. F2 is introduced into UM4 together with water. F2 and water are brought into contact at a temperature in the range of 10 to 95 °C. A mixture M4 is obtained, which mixture comprises an aqueous phase PA(4) and an organic phase PO(4), the pH of the aqueous phase PA(4) of M4 being in the range of 7.5 to 11 and the pH of PA(4) < the pH of PA(1). Then M4 is introduced into US4, optionally passing through USL4 before being introduced into US4. A stream F4 containing purified pyrolysis oil is obtained. A further stream FA(4) containing PA(4) is also obtained. Then F4 can be stored or transferred for further processing. Optionally, the aqueous stream, which is FA(4), is recycled in UM2 (not shown).

[0010] Optionally, the Z of the unit WIt further comprises a washing unit UM3 and a liquid-liquid separation unit US3, which further comprises a solid-liquid separation unit SL3, SLS3 located downstream of UM3 if present, and US3 located downstream of SLS3. Thus, F2 is introduced into UM3 (not UM4) together with water. F2 and water are brought into contact at a temperature in the range of 10 to 95°C. A mixture M3 is obtained, and the mixture is divided into an aqueous phase P A (3) and organic phase P O (3) including the aqueous phase P of M3 A (3) The pH is in the range of 7.5 to 11, P A (3) PH <P A (1) This is the pH. Next, M3 is introduced into US3, but in some cases it passes through USL3 before being introduced into US3. A flow F3 containing refined pyrolysis oil is obtained. P A (3) Further flow F A (3) is also obtained. Next, F3 is introduced into UM4 together with water. F3 and water are brought into contact at a temperature in the range of 10 to 95°C. A mixture M4 is obtained, and the mixture is the aqueous phase P A (4) and organic phase P O (4) including the aqueous phase P of M4 A (4) The pH is in the range of 7.5 to 11, P A (4) PH <P A (1) This is the pH. Next, M4 is introduced into US4, but in some cases it passes through USL4 before being introduced into US4. A flow F4 containing refined pyrolysis oil is obtained. P A (4) Further flow F A (4) is also obtained. F4 can then be stored or transferred for further processing. Depending on the case, F A (4) The aqueous flow is recycled in UM2 and / or UM3 (not shown). In some cases, F A (3) The aqueous flow is recycled in UM2 (not shown). In some cases, F A (2) The water flow is recycled in UM1 (not shown). [Modes for carrying out the invention]

[0011] Generally, 1 to 100% by weight, 5 to 100% by weight, 10 to 100% by weight, 20 to 100% by weight, 30 to 100% by weight, 40 to 100% by weight, 50 to 100% by weight, 60 to 100% by weight, 70 to 100% by weight, 80 to 100% by weight, or 90 to 100% by weight of F0 may consist of pyrolysis oil.

[0012] Preferably 95 to 100% by weight, more preferably 98 to 100% by weight, and more preferably 99 to 100% by weight of F0 consists of pyrolysis oil.

[0013] 99.5 to 100% by weight of F0, or 99.8 to 100% by weight, or 99.9% by weight may consist of pyrolysis oil.

[0014] In the context of the present invention, the refined pyrolysis oil may have any oxygen content.

[0015] Preferably, the pyrolysis oil according to (i) has a total acid number (TAN) in the range of 0.5 to 60 Mg KOH / g(F0), more preferably in the range of 1 to 40 Mg KOH / g(F0), and more preferably in the range of 3 to 20 Mg KOH / g(F0), as determined as described in Reference Example 3.

[0016] Preferably, the pyrolysis oil according to (i) has an oxygen content in the range of 0 to 15 g(O) / 100 g(F0), more preferably in the range of 0.5 to 10 g(O) / 100 g(F0), more preferably in the range of 0.5 to 5 g(O) / 100 g(F0), and more preferably in the range of 0.5 to 2 g(O) / 100 g(F0), as determined as described in Reference Example 4.

[0017] Preferably, the pyrolysis oil according to (i) has a total chlorine content in the range of 30 to 3,000 WPPM (ppm by weight), more preferably 30 to 500 WPPM, and more preferably 30 to 300 WPPM, as determined as described in Reference Example 1.1.

[0018] Preferably, the pyrolysis oil according to (i) has a chloride content in the range of at most 40 WPPM, more preferably 0 to 30 WPPM, as determined as described in Reference Example 1.2.

[0019] Preferably, the pyrolysis oil according to (i) has a nitrogen content in the range of 50 to 20,000 WPPM (ppm by weight), more preferably 50 to 5,000 WPPM, and more preferably 100 to 4,000 WPPM, as determined as described in Reference Example 2.

[0020] Preferably, the pyrolysis oil according to (i) has an iron content in the range of 1 to 100 WPPM (ppm by weight), preferably 10 to 50 WPPM, as determined as described in Reference Example 6.

[0021] Preferably, the pyrolysis oil according to (i) has a zinc content in the range of 1 to 100 WPPM (ppm by weight), preferably 1 to 50 WPPM, as determined as described in Reference Example 6.

[0022] Preferably, the pyrolysis oil according to (i) has a tin content in the range of 1 to 100 WPPM (ppm by weight), preferably 1 to 50 WPPM, as determined as described in Reference Example 6.

[0023] Preferably, the pyrolysis oil provided in (i) is obtained from the pyrolysis of waste material, the waste material being plastic waste material, tire waste material, or biomass waste.

[0024] Preferably, (i) is (i.1) Includes the step of removing pyrolysis oil from a storage tank or truck.

[0025] Preferably, (ii.2) is (ii.2.1)Z E The process involves introducing water into the UM1 provided there, (ii.2.2) A step of bringing F0 into contact with water, more preferably mixing it, and adding it to UM1 to obtain a mixture PM1 containing water and pyrolysis oil, (ii.2.3) B is introduced into UM1, and B is brought into contact with the mixture PM1 obtained in (ii.2.2), more preferably mixed, and introduced into UM1 to form the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of is in the range of 7.5 to 11, more preferably in the range of 8 to 10, and the process Includes.

[0026] Preferably, (ii.2) is, (ii.2.1)Z E The process involves introducing water into the UM1 provided there, (ii.2.2) Bring F0 into contact with water, more preferably mixed, and Z E A step of obtaining a mixture PM1 containing water and pyrolysis oil by placing it in a container, wherein the aqueous phase of PM1 has a pH value of PH(PM1) measured by a pH sensor of UM1, (ii.2.3) By bringing B into contact with M1 obtained in (ii.2.2), more preferably mixing them, and introducing B into UM1, the pH of the aqueous phase of PM1 is adjusted, and the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) PH > PH(PM1), P A (1) The pH of is in the range of 7.5 to 11, more preferably in the range of 8 to 10, and the process Includes.

[0027] Alternatively, preferably, (ii.2) is, (ii.2.1') ​​A step of mixing water and B to obtain a mixture M0 of water and B having a pH (M0) in the range of 12 to 14, The M0 obtained according to (ii.2.2')(ii.2.1') ​​is introduced into UM1, F0 is brought into contact with M0, and more preferably mixed to form the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of is in the range of 7.5 to 11, more preferably in the range of 8 to 10, and the process Includes.

[0028] In the context of the present invention, preferably, the extraction unit UM1 is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel.

[0029] In the context of the present invention, those skilled in the art will know, according to their general knowledge, the temperature to apply for contacting the flow F0 in the liquid phase, water, and base B, depending on the properties / type of the pyrolysis oil.

[0030] Preferably, the contact step, preferably the mixing step, is carried out in accordance with (ii.2) at a temperature T1 in the range of 10 to 95°C, more preferably in the range of 15 to 85°C, and more preferably in the range of 20 to 80°C.

[0031] Preferably, the contact step, more preferably the mixing step, is carried out according to (ii.2) at a pressure P1 in the range of 0.8 to 1.2 bar (ABS), more preferably in the range of 0.9 to 1.1 bar (ABS). More preferably, when T1 ≤ 95°C, the contact step, more preferably the mixing step, is carried out according to (ii.2) at a pressure P1 in the range of 0.8 to 1.2 bar (ABS), more preferably in the range of 0.9 to 1.1 bar (ABS), more preferably about 1 bar (ABS).

[0032] Alternatively, the contact step, more preferably the mixing step, in accordance with (ii.2) is performed at a pressure P1 in the range of 0.5 to 5 bar (ABS), more preferably in the range of 0.7 to 3 bar (ABS), and more preferably in the range of 0.9 to 2 bar (ABS).

[0033] In the context of the present invention, when T1 > 95°C, the pressure P1 is in the range of 1 to 16 bar (ABS).

[0034] Preferably, base B is one or more of alkali metal compounds, alkaline earth metal compounds (e.g., alkaline earth metal oxides and / or hydroxides, e.g., calcium hydroxide), and ammonia. More preferably, B is an alkali metal compound which is 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; and more preferably potassium hydroxide.

[0035] Alternatively, base B is one or more potassium compounds, more preferably one or more of potassium hydroxide, potassium bicarbonate, and potassium carbonate, more preferably potassium hydroxide or potassium carbonate, and more preferably potassium hydroxide.

[0036] Preferably, the water used in (ii) is desalinated water.

[0037] Preferably, according to (ii.2), the weight ratio of water to F0 is in the range of 0.05:1 to 2:1, more preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, more preferably in the range of 0.1:1 to 0.5:1, more preferably in the range of 0.2:1 to 0.5:1, more preferably in the range of 0.25:1 to 0.5:1, and more preferably in the range of 0.3:1 to 0.5:1.

[0038] Preferably, the liquid-liquid separation unit US1 is one or more of a hydrocyclone, a sedimentation tank, and a centrifuge, more preferably a decanter, a hydrocyclone, a sedimentation tank, or a centrifuge, and more preferably a sedimentation tank.

[0039] In the context of the present invention, UM1 and US1 are two different units.

[0040] Preferably, the separation in US1 according to (ii.3) is carried out at a temperature in the range of 10 to 95°C, more preferably in the range of 15 to 85°C, and more preferably in the range of 20 to 80°C.

[0041] Preferably, before passing M1 through US1 according to (ii.3), the process further includes passing M1 through a solid-liquid separation unit SLS1 to remove solids in M1, if present.

[0042] Preferably, the solid-liquid separation unit SLS1 is one or more of a filter and a centrifuge.

[0043] Solid-liquid separation can be performed using a filter that uses differential pressure as the driving force, or it can be performed using a centrifuge that separates liquids and solids by centrifugal force.

[0044] The use of filters often implies discontinuous solid-liquid separation, where the pressure difference increases with increasing filtration time. After a certain pressure difference or filtration time, the solid must be removed from the filter by backflushing with fluid, gas, or a mixture of both (e.g., waste filter, backflushing filter), by an automated system (e.g., automatic cleaning filter), or by rotation or vibration (e.g., pressure leaf filter, candle filter, filter press). During solid removal, a second parallel filter is initiated until a certain pressure difference or filtration time is reached, at which point the filter that has emptied the solid resumes operation.

[0045] Filtration can be performed using a waste filter (e.g., a bag filter, a filter sheet, or a membrane filter) where solids are removed by backflushing, or solids remain on the filter cloth, resulting in filter replacement after a certain pressure difference or operating time.

[0046] Filtration can be assisted by using filter aids to improve filtration behavior. This may lead to the potential use of continuous filters (e.g., belt filters, drum filters).

[0047] Centrifugal separators can be used for discontinuous or continuous solid-liquid separation, depending on the type of centrifuge. Centrifugal separators (e.g., decanter centrifuges, separator centrifuges) can be used in two-phase (solid-liquid) or three-phase systems of two liquid phases and a solid to separate solids from one or more liquids, and separate liquids from liquids. Compared to decanter centrifuges, where solids are continuously separated and removed, in separator centrifuges, the solids must be released after the centrifuge is loaded to its maximum solid (discontinuous) capacity. Centrifugation can be assisted by the use of coagulants to improve the centrifugal behavior.

[0048] Alternatively, preferably, no separation unit is located between UM1 and US1. In this case, M1 removed from UM1 is passed directly to US1.

[0049] Units UM1 and US1 may be juxtaposed to form, for example, a mixer settra.

[0050] Preferably, this process is In the separation unit USA1, preferably in the sedimentation tank, P obtained according to (ii.3) A Flow F including (1) A The process further includes obtaining an aqueous flow SA1 containing water through (1).

[0051] Preferably, the process further includes one or more purification steps for purifying SA1.

[0052] Preferably, the process further includes a step of recycling SA1 in UM1, more preferably purified SA1 (water).

[0053] F A (1) preferably consists of 80 to 100% by weight, more preferably 85 to 100% by weight of water.

[0054] Alternatively, preferably, this process is F obtained according to (ii.3) A (1) further includes a step of recycling at least a portion of the water contained in UM1.

[0055] In the context of the present invention, preferably, no organic solvent is used in (ii).

[0056] The process may further include an acidic treatment after (ii) and before (iii). In particular, the acidic treatment may include adding one or more acidic components to F1.

[0057] (ii) of the present invention is Z E This may include one or more subsequent extractions within the process.

[0058] Preferably, this process is performed in US1 P A (1) and P O If a precipitate forms at the interface with (1), the process further includes purging the precipitate from US1.

[0059] Preferably, US1 is P A (1) and P O (1) comprises means for purging any optional precipitate formed at the interface with (1).

[0060] Preferably, the purged precipitate is subjected to one or more purification processes. For example, the precipitate can be processed with a filter and / or centrifuge.

[0061] With respect to (iii), according to the first option, (iii) is preferably, (iii.1) F1 to Z W The process involves introducing the material into the cleaning unit UM2 provided therein, (iii.2) F1 is brought into contact with water in UM2 at a temperature T2 in the range of 10 to 95°C, and the aqueous phase P A (2) and organic phase P O (2) A step to obtain a mixture M2 comprising the aqueous phase P of M2 A (2) The pH is in the range of 7.5 to 11, P A (2) PH <P A (1) The pH of the process, The mixture M2 obtained according to (iii.3)(iii.2) is Z W It is provided and passes through the liquid-liquid separation unit US2 located downstream of UM2, P A Flow F including (2) A (2) and P, which is a refined pyrolysis oil. O (2) A process to obtain flow F2 including (2) Includes.

[0062] Preferably, the present invention is a process for refining pyrolysis oil, (i) A step of providing a flow F0 containing pyrolysis oil, (ii) Take the flow F0 provided in (i) into at least one extraction zone Z E A step of subjecting to extraction to obtain a flow F1 containing the extracted pyrolysis oil, wherein (ii) is (ii.1) Set F0 to Z E The process of introducing the contents into the extraction unit UM1 provided therein, (ii.2) F0 is brought into contact with water and base B in UM1 at a temperature T1 in the range of 10 to 200°C, and the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A(1) The pH of the process is in the range of 7.5 to 11. The mixture M1 obtained according to (ii.3)(ii.2) is Z E It is provided and passes through the liquid-liquid separation unit US1 located downstream of UM1, P A Flow F including (1) A (1) and P, which is extracted pyrolysis oil. O (1) A process to obtain flow F1 including, (ii.4)Z E A process including the step of removing F1 from, (iii)(ii) The flow F1 provided in Z E At least one washing zone Z located downstream W The process involves washing to obtain a flow F2 containing refined pyrolysis oil, wherein (iii) is (iii.1) F1 to Z W The process of introducing the contents into the cleaning unit UM2 provided therein, (iii.2) F1 is brought into contact with water in UM2 at a temperature T2 in the range of 10 to 95°C, and the aqueous phase P A (2) and organic phase P O (2) A step to obtain a mixture M2 comprising the aqueous phase P of M2 A (2) The pH is in the range of 7.5 to 11, P A (2) PH <P A (1) The PH of the process, The mixture M2 obtained according to (iii.3)(iii.2) is Z W It is provided and passes through the liquid-liquid separation unit US2 located downstream of UM2, P A Flow F including (2) A (2) and P, which is a refined pyrolysis oil. O (2) A process to obtain a flow F2 including, and This includes processes related to the process.

[0063] Such alternative forms are shown in Figures 1, 2, and 4.

[0064] Preferably, the washing unit UM2 is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel.

[0065] Preferably, according to (iii.2), the weight ratio of water to F1 is in the range of 0.05:1 to 2:1, more preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, and more preferably in the range of 0.1:1 to 0.5:1.

[0066] Preferably, when B is KOH or NaOH, the weight ratio of water to F1 is in the range of 0.05:1 to 2:1, more preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, and more preferably in the range of 0.1:1 to 0.5:1.

[0067] Preferably, T2 is in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

[0068] Preferably, T1 ≤ T2 ≤ 1.25 T1, and more preferably, T1 ≤ T2 ≤ 1.1 T1.

[0069] Preferably, the water used in (iii) is desalinated water.

[0070] Preferably, the liquid-liquid separation unit US2 is one or more of a hydrocyclone, a sedimentation tank, and a centrifuge, more preferably a hydrocyclone, a sedimentation tank, or a centrifuge, and more preferably a sedimentation tank or a centrifuge.

[0071] Preferably, UM2 and US2 are two different units.

[0072] Preferably, the separation in US2 according to (iii.3) is carried out at a temperature in the range of 10 to 85°C, more preferably in the range of 15 to 85°C, and more preferably in the range of 20 to 80°C.

[0073] Depending on the circumstances, this process may be performed before passing M2 through US2 in accordance with (iii.3). If present, the process further includes passing M2 through a solid-liquid separation unit SLS2 to remove solids in M2.

[0074] Preferably, the solid-liquid separation unit SLS2 is one or more of a filter and a centrifuge.

[0075] Solid-liquid separation can be performed using a filter that uses differential pressure as the driving force, or it can be performed using a centrifuge that separates liquids and solids by centrifugal force.

[0076] The use of filters often implies discontinuous solid-liquid separation, where the pressure difference increases with increasing filtration time. After a certain pressure difference or filtration time, the solid must be removed from the filter by backflushing with fluid, gas, or a mixture of both (e.g., waste filter, backflushing filter), by an automated system (e.g., automatic cleaning filter), or by rotation or vibration (e.g., pressure leaf filter, candle filter, filter press). During solid removal, a second parallel filter is initiated until a certain pressure difference or filtration time is reached, at which point the filter that has emptied the solid resumes operation.

[0077] Filtration can be performed using a waste filter (e.g., a bag filter, a filter sheet, or a membrane filter) where solids are removed by backflushing, or solids remain on the filter cloth, resulting in filter replacement after a certain pressure difference or operating time.

[0078] Filtration can be assisted by using filter aids to improve filtration behavior. This may lead to the potential use of continuous filters (e.g., belt filters, drum filters).

[0079] A centrifuge can be used for discontinuous or continuous solid-liquid separation depending on the type of centrifuge. Centrifuges (e.g., decanter centrifuges, separator centrifuges) can be used in two-phase (solid-liquid) or three-phase systems of two liquid phases and solids to separate solids from one or more liquids and to separate liquids from each other. Compared to a decanter centrifuge where solids are continuously separated and removed, in a separator centrifuge, the solids must be discharged after the centrifuge has been loaded to its maximum solids (discontinuous). Centrifugation can be assisted by the use of flocculants to improve the centrifugation behavior.

[0080] [[ID='4']]Alternatively, preferably, no separation unit is located between UM2 and US2. In this regard, M2 removed from UM2 is passed directly to US2.

[0081] The units UM2 and US2 can be considered to be juxtaposed, for example, to form a mixer settler.

[0082] Preferably, the process is P in US2 A (2) and P O When a precipitate is formed at the interface between (2) and P(2), the method further includes purging the precipitate from US2.

[0083] Regarding (iii), according to the second option, (iii) preferably (iii.1’) Introducing F1 into an extraction column UM + US provided in Z W ; and (iii.2’) Introducing water into UM + US; and (iii.3’) Contacting F1 with water at a temperature T2’ in the range of 10 to 95 °C in UM + US to obtain a stream F(2) containing an aqueous phase P(2) (the pH of the aqueous phase P(2) of M2 is in the range of 7.5 to 11, and the pH of P(2) < the pH of P(1)), and obtaining a stream F2 containing purified pyrolysis oil. A (2) to obtain a flow rate F A (2) (the aqueous phase P of M2 A (2) has a pH in the range of 7.5 to 11, and P A (2) pH < P A (1) pH), obtaining a stream F2 containing purified pyrolysis oil) It includes. Such an alternative form is shown in FIG. 3.

[0084] Preferably, the present invention is a process for purifying pyrolysis oil, comprising: (i) providing a stream F0 containing pyrolysis oil; (ii) subjecting the stream F0 provided in (i) to extraction in at least one extraction zone Z E to obtain a stream F1 containing the extracted pyrolysis oil, wherein (ii) comprises: (ii.1) introducing F0 into an extraction unit UM1 provided in Z E ; (ii.2) contacting F0 with water and a base B in UM1 at a temperature T1 in the range of 10 to 200 °C to obtain a mixture M1 containing an aqueous phase P A (1) and an organic phase P O (1), wherein the pH of the aqueous phase P A (1) of M1 is in the range of 7.5 to 11; (ii.3) passing the mixture M1 obtained according to (ii.2) through a liquid-liquid separation unit US1 provided in Z E and located downstream of UM1 to obtain a stream F A (1) containing P A (1) and a stream F1 containing P O (1) which is the extracted pyrolysis oil; (ii.4) removing F1 from Z E ; and (iii) subjecting the stream F1 provided in (ii) to washing in at least one washing zone Z E located downstream of Z W to obtain a stream F2 containing purified pyrolysis oil, wherein (iii) comprises: (iii.1’) introducing F1 into an extraction column UM+US provided in Z W ; (iii.2’) introducing water into UM+US; (iii.3’) contacting F1 with water in UM+US at a temperature T2’ in the range of 10 to 95 °C to obtain a stream F A (2) containing an aqueous phase P A (2) (the aqueous phase P of M2A (2) The pH is in the range of 7.5 to 11, P A (2) PH <P A (1) A step of obtaining a flow F2 containing refined pyrolysis oil at pH (1) and This includes processes related to the process.

[0085] Preferably, according to (iii.3'), the weight ratio of water to F1 is in the range of 0.05:1 to 2:1, more preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, and more preferably in the range of 0.1:1 to 0.5:1.

[0086] Preferably, T2' is in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

[0087] Preferably, T1 ≤ T2' ≤ 1.25 T1, and more preferably, T1 ≤ T2' ≤ 1.1 T1.

[0088] Preferably, (iii) is performed at a pressure P2 in the range of 0.75 to 1.25 bar (ABS), more preferably in the range of 0.9 to 1.1 bar (ABS), and more preferably about 1 bar (ABS).

[0089] F A (2) preferably 90 to 100% by weight, more preferably 95 to 100% by weight, consists of water.

[0090] In the context of the present invention, this process is F obtained according to (iii.3) A (2) A process of recycling at least a portion of the water contained in (ii.2) and / or (iii.2), or F obtained according to (iii.3') A (2) A process to recycle at least a portion of the water contained in (ii.2) and / or (iii.2'). It is preferable to further include the following.

[0091] Preferably, F obtained according to (iii.3) A The process of recycling at least a portion of the water contained in (2) in (ii.2) and / or (iii.2) is obtained according to (iii.3) F A (2) includes the step of passing at least a portion of the water contained in UM1 and / or UM2.

[0092] Preferably, F obtained according to (iii.3') A The step of recycling at least a portion of the water contained in (2) in (ii.2) and / or (iii.2') is obtained according to (iii.3') F A (2) includes the step of passing at least a portion of the water contained in UM1 and / or UM+US.

[0093] Preferably, the water used in (iii) is desalinated water.

[0094] Preferably, no organic solvent is used in (iii).

[0095] Preferably, in (iii), no base is added, and the base is one or more of alkali metal compounds (e.g., 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), alkaline earth metal compounds, and ammonia.

[0096] Preferably, the stream F2 containing the refined pyrolysis oil obtained according to (iii) has a TAN lower than the total acid number (TAN) of the pyrolysis oil provided in (i).

[0097] Preferably, the stream F2 containing the refined pyrolysis oil obtained according to (iii) has a TAN in the range of 0 to 20 Mg KOH / g(F2), more preferably in the range of 0 to 10 Mg KOH / g(F2), and more preferably in the range of 0 to 4 Mg KOH / g(F2), as determined as described in Reference Example 3.

[0098] Preferably, the stream F2 containing the refined pyrolysis oil obtained according to (iii) has an oxygen content less than or equal to, and more preferably less than, that of the pyrolysis oil provided in (i).

[0099] Preferably, the stream F2 containing the refined pyrolysis oil has an oxygen content in the range of 0 to 2 g(O) / 100 g(F2), as determined as described in Reference Example 4.

[0100] According to the present invention, it is preferable that the flow F2 containing the refined pyrolysis oil obtained according to (iii) has a reduced iron content compared to the pyrolysis oil provided in (i). For example, the reduction in iron (FE) content in F2 compared to the pyrolysis oil provided in (i) may be in the range of 1 to 100%, or 5 to 95%, or 40 to 90%.

[0101] According to the present invention, the flow F2 containing the refined pyrolysis oil obtained according to (iii) is considered to have a reduced total chlorine content and / or chloride content compared to the pyrolysis oil provided in (i). For example, the reduction in total chlorine content and / or chloride content in F2 compared to the pyrolysis oil provided in (i) may be in the range of 1 to 100%, or 1 to 80%, or 10 to 50%.

[0102] According to the present invention, the flow F2 containing the refined pyrolysis oil obtained according to (iii) is considered to have a reduced tin (SN) content compared to the pyrolysis oil provided in (i). For example, the reduction in tin content in F2 compared to the pyrolysis oil provided in (i) may be in the range of 1 to 100%, or 5 to 80%, or 20 to 80%.

[0103] According to the present invention, the flow F2 containing the refined pyrolysis oil obtained according to (iii) is considered to have a reduced zinc (Zn) content compared to the pyrolysis oil provided in (i). For example, the reduction in zinc content in F2 compared to the pyrolysis oil provided in (i) may be in the range of 1 to 100%, or 5 to 80%, or 20 to 80%.

[0104] According to the present invention, the flow F2 containing the refined pyrolysis oil obtained according to (iii) is considered to have a lower nitrogen content than the pyrolysis oil provided in (i).

[0105] According to the present invention, the stream F2 containing the refined pyrolysis oil obtained according to (iii) is considered to have a lower sulfur content than the pyrolysis oil provided in (i).

[0106] Preferably 95 to 100% by weight, more preferably 98 to 100% by weight, more preferably 99 to 100% by weight, and more preferably 99.5 to 100% by weight of F2 consists of refined pyrolysis oil.

[0107] Depending on the circumstances, the present invention process may be Z W This further includes one or more subsequent washes inside. According to this option, this process is (iv)(iii) At least a portion of the flow F2 obtained according to Z W (iv) further includes subjecting to one or more subsequent washes in (iv.1) Depending on the case, at least a portion of F2 obtained according to (iii), preferably F2, Z W It is equipped and introduced into the washing unit UM3 located downstream of US2, At least a portion of F2, preferably F2, is brought into contact with water in UM3 at a temperature T3 ranging from 10 to 95°C, forming an aqueous phase P A (3) and organic phase P O (3) is included and ranges from 7.5 to 11, P A (3) PH <P A (1) A mixture M3 with the pH of (1) is obtained. ZW In the liquid-liquid separation unit US3 located downstream of UM3, the mixture M3 is passed through P A Flow F including (3) A (3) and P, which is a refined pyrolysis oil. O (3) A process to obtain flow F3 including, At least a portion of F2 obtained according to (iv.2)(iii), preferably F2, or at least a portion of F3 obtained according to (iv.1), preferably F3, Z W The process involves preparing for and introducing the solution into the washing unit UM4 located downstream of US3, (iv.3) At least a portion of F2, preferably F2, or at least a portion of F3, preferably F3, is brought into contact with water in UM4 at a temperature T4 in the range of 10 to 95°C, forming an aqueous phase P A (4) and organic phase P O (4) A step to obtain a mixture M4 containing the aqueous phase P of M4 A (4) The pH is in the range of 7.5 to 11, P A (4) PH <P A (1) The pH of the process, The mixture M4 obtained according to (iv.4)(iv.3) is Z W It is provided and passes through the liquid-liquid separation unit US4 located downstream of UM4, P A Flow F including (4) A (4) and P, which is a refined pyrolysis oil. O (4) A process to obtain flow F4 including (4) Includes.

[0108] The aforementioned options are shown, for example, in Figure 4.

[0109] Preferably, P A (3) PH <P A (2) This is the pH.

[0110] Preferably, P A (4) PH <P A (2) This is the pH.

[0111] Preferably, P A(4) PH <P A (3) is PH. More preferably, P A (4) PH <P A (3) PH <P A (2) PH <P A This is the pH of (1).

[0112] Preferably, according to the above options, the process is F A (4) further includes a step of recycling at least a portion of the above into UM2 and / or UM3 (if any).

[0113] F A (4) preferably consists of 90 to 100% by weight, more preferably 95 to 100% by weight, of water.

[0114] Preferably, UM4, if present, is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel.

[0115] Preferably, according to (iv.3), the weight ratio of water to at least a portion of F2, more preferably F2, or at least a portion of F3, more preferably F3, is in the range of 0.05:1 to 2:1, more preferably 0.1:1 to 1.5:1, more preferably 0.1:1 to 1.2:1, and more preferably 0.1:1 to 0.5:1.

[0116] Preferably, T4 is in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

[0117] Preferably, T1 ≤ T4 ≤ 1.25 T1, and more preferably, T1 ≤ T4 ≤ 1.1 T1.

[0118] Preferably, the liquid-liquid separation unit US4 is one or more of a hydrocyclone, a sedimentation tank, and a centrifuge, more preferably a hydrocyclone, a sedimentation tank, or a centrifuge, and more preferably a sedimentation tank or a centrifuge.

[0119] Preferably, UM4 and US4 are two different units.

[0120] Preferably, the separation in US4 according to (iv.4) is carried out at a temperature in the range of 10 to 85°C, more preferably in the range of 15 to 85°C, and more preferably in the range of 20 to 80°C.

[0121] Preferably, before passing through M4 in US4 according to (iv.4), this process If present, the process further includes passing the M4 through a solid-liquid separation unit SLS4 to remove any solids in the M4.

[0122] Preferably, the solid-liquid separation unit SLS4 is one or more of a filter and a centrifuge.

[0123] Solid-liquid separation can be performed by a filter that uses differential pressure as the driving force, or by a centrifuge that separates liquids and solids by centrifugal force. The use of a filter often implies discontinuous solid-liquid separation, where the pressure difference increases with increasing filtration time. After a certain amount of pressure difference or filtration time, the solid must be removed from the filter by backflushing with fluid or gas or a mixture of both (e.g., waste filter, backflushing filter), by an automatic system (e.g., automatic cleaning filter), or by rotation or vibration (e.g., pressure leaf filter, candle filter, filter press). During solid removal, a second parallel filter is started to operate until a certain pressure difference or filtration time is reached, at which point the filter that has emptied the solid starts operating again.

[0124] Filtration can be performed using a waste filter (e.g., a bag filter, a filter sheet, or a membrane filter) where solids are removed by backflushing, or solids remain on the filter cloth, resulting in filter replacement after a certain pressure difference or operating time.

[0125] Filtration can be assisted by using filter aids to improve filtration behavior. This may lead to the potential use of continuous filters (e.g., belt filters, drum filters).

[0126] Centrifugal separators can be used for discontinuous or continuous solid-liquid separation, depending on the type of centrifuge. Centrifugal separators (e.g., decanter centrifuges, separator centrifuges) can be used in two-phase (solid-liquid) or three-phase systems of two liquid phases and a solid to separate solids from one or more liquids, and separate liquids from liquids. Compared to decanter centrifuges, where solids are continuously separated and removed, in separator centrifuges, the solids must be released after the centrifuge is loaded to its maximum solid (discontinuous) capacity. Centrifugation can be assisted by the use of coagulants to improve the centrifugal behavior.

[0127] Alternatively, preferably, no separation unit is located between UM4 and US4. In this case, M4 removed from UM4 is passed directly to US4.

[0128] Preferably, if (iv.1) is performed, this process F A (3) Further includes a step of recycling at least a portion of the above into UM2.

[0129] F A (3) preferably consists of 90 to 100% by weight, more preferably 95 to 100% by weight, of water.

[0130] Preferably, UM3, if present, is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel.

[0131] Preferably, according to (iv.1), the weight ratio of water to at least a portion of F2, more preferably F2, is in the range of 0.05:1 to 2:1, more preferably 0.1:1 to 1.5:1, more preferably 0.1:1 to 1.2:1, and more preferably 0.1:1 to 0.5:1.

[0132] Preferably, T3 is in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

[0133] Preferably, T1 ≤ T3 ≤ 1.25 T1, and more preferably, T1 ≤ T3 ≤ 1.1 T1.

[0134] Preferably, the liquid-liquid separation unit US3 is one or more of a hydrocyclone, a sedimentation tank, and a centrifuge, more preferably a hydrocyclone, a sedimentation tank, or a centrifuge, more preferably a sedimentation tank or a centrifuge.

[0135] Preferably, UM3 and US3 are two different units.

[0136] Preferably, the separation in US3 according to (iv.1) is carried out at a temperature in the range of 10 to 85°C, more preferably in the range of 15 to 85°C, and more preferably in the range of 20 to 80°C.

[0137] Preferably, before passing through M3 in US3 according to (iv.1), this process If present, the process further includes passing the M3 through a solid-liquid separation unit SLS3 to remove any solids in the M3.

[0138] Preferably, the solid-liquid separation unit SLS3 is one or more of a filter and a centrifuge.

[0139] Alternatively, preferably, no separation unit is located between UM3 and US3. In this case, M3 removed from UM3 is passed directly to US3.

[0140] Preferably, the water used in (iv) is desalinated water.

[0141] Preferably, no organic solvent is used in (iv).

[0142] Preferably, no base is added in (iv), and the base is one or more of alkali metal compounds (e.g., 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), alkaline earth metal compounds, and ammonia.

[0143] Preferably, (iv) is performed at a pressure P3 in the range of 0.75 to 1.25 bar (ABS), more preferably in the range of 0.9 to 1.1 bar (ABS), and more preferably about 1 bar (ABS).

[0144] In the context of the present invention, this process is The further step includes introducing F2 containing the pyrolysis oil obtained according to (v)(iii), and optionally F4 obtained according to (iv), into at least one storage unit SU, and storing the pyrolysis oil in the SU.

[0145] Preferably, the storage unit SU is a storage tank, more preferably made of one or more of steel and stainless steel, and more preferably carbon steel and stainless steel.

[0146] Preferably, the process of the present invention is The process further includes one or more of the following steps: dechlorination, hydrogenation, hydrotreatment, steam decomposition, hydrocracking, adsorption, distillation, stripping, and aqueous extraction.

[0147] Preferably, the process of the present invention is a continuous or semi-continuous process.

[0148] Preferably, the process of the present invention comprises (i), (ii), (iii), and optionally (iv) and optionally (v).

[0149] The present invention further comprises a unit for carrying out a process for refining pyrolysis oil according to the present invention, - At least one extraction zone Z comprising an extraction unit UM1 and a liquid-liquid separation unit US1 E Therefore, UM1 is located upstream of US1, in extraction zone Z. E and, -F0 to Z E An entry point for introducing it, -Z E An exit means for removing F1 from, - An entry point for introducing F0 into UM1, - An exit means for removing M1 from UM1, - An entry point for introducing M1 into US1, - An exit strategy from removing F1 from US1, -Z E At least one washing zone Z located downstream W and, -F1 to Z W An entry point for introducing it, -Z W An exit means for removing F2 from and Regarding a unit that includes the following:

[0150] Preferably, US1 is P A (1) and P O (1) comprises means for purging any optional precipitate formed at the interface with (1).

[0151] Preferably, according to the first option, Z W teeth, - Cleaning unit UM2, -Liquid-liquid separation unit US2, wherein UM2 is located upstream of US2, - An entry point for introducing F1 into UM2, - An inlet for introducing water into UM2, - An exit means for removing M2 from UM2, - An entry point for introducing US2 to M2, - An exit strategy from removing F2 from US2 It is equipped with.

[0152] Depending on the case, Z W The system further comprises a washing unit UM4, preferably a mixing unit and a liquid-liquid separation unit US4, where UM4 is located downstream of US2 and US4 is located downstream of UM4.

[0153] Depending on the case, Z W The system further comprises a washing unit UM3, preferably a mixing unit and a liquid-liquid separation unit US3, where UM3 is located downstream of US2 and upstream of UM4, and US3 is located downstream of UM3 and upstream of UM4.

[0154] Preferably, according to the second option, Z W teeth, - Extraction column UM+US and, - An entry point for introducing F1 into UM+US, - An inlet for introducing water into UM+US, - An exit method from removing F2 from UM+US It is equipped with.

[0155] In the context of the present invention, preferably, the unit is It further comprises one or more of the following: storage tanks, cracking zones, dechlorination zones, hydrogenation zones, hydrogenation treatment zones, stripping zones, and distillation zones.

[0156] The present invention further relates to refined pyrolysis oil that can be obtained or obtained by the process according to the present invention.

[0157] Preferably, the refined pyrolysis oil of the present invention has a total acid number (TAN) in the range of 0 to 20 Mg KOH / g(oil), more preferably in the range of 0 to 10 Mg KOH / g(oil), more preferably in the range of 0 to 4 Mg KOH / g(oil), more preferably in the range of 0 to 1 Mg KOH / g(oil), and more preferably less than 0 to 1 Mg KOH / g(oil), as determined as described in Reference Example 3.

[0158] Preferably, the refined pyrolysis oil of the present invention has an oxygen content in the range of 0 to 2 g(O) / 100 g(oil), as determined as described in Reference Example 4.

[0159] The present invention is further described by the following set of embodiments and combinations of embodiments arising from the dependencies and backreferences shown. In particular, it should be noted that in each example in which the scope of an embodiment is referred to, for example in the context of the term, for example, “any one process of Embodiments 1 to 4,” all embodiments within this scope are expressly disclosed to those skilled in the art; that is, the wording of this term should be understood by those skilled in the art as synonymous with “any one process of Embodiments 1, 2, 3, and 4.” Furthermore, it should be explicitly noted that the following set of embodiments represents a well-structured portion of a general description directed toward preferred aspects of the present invention and therefore adequately supports, but does not represent, the claims of the present invention.

[0160] 1. A process for refining pyrolysis oil, (i) A step of providing a flow F0 containing pyrolysis oil, (ii) Take the flow F0 provided in (i) into at least one extraction zone Z E A step of subjecting to extraction to obtain a flow F1 containing the extracted pyrolysis oil, wherein (ii) is (ii.1) Set F0 to Z E The process of introducing the contents into the extraction unit UM1 provided therein, (ii.2) F0 is brought into contact with water and base B in UM1 at a temperature T1 in the range of 10 to 200°C, and the aqueous phase PA (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of the process is in the range of 7.5 to 11. The mixture M1 obtained according to (ii.3)(ii.2) is Z E It is provided and passes through the liquid-liquid separation unit US1 located downstream of UM1, P A Flow F including (1) A (1) and P, which is extracted pyrolysis oil. O (1) A process to obtain flow F1 including, (ii.4)Z E A process including the step of removing F1 from, (iii)(ii) The flow F1 provided in Z E At least one washing zone Z located downstream W The process involves subjecting the material to cleaning to obtain a flow F2 containing refined pyrolysis oil. A process that includes this.

[0161] 2. The process according to Embodiment 1, wherein 95 to 100% by weight, preferably 98 to 100% by weight, and more preferably 99 to 100% by weight of F0 consists of pyrolysis oil.

[0162] The process according to Embodiment 1 or 2, wherein the pyrolysis oil according to 3.(i) has an oxygen content in the range of 0.5 to 15 g(O) / 100 g(F0), preferably in the range of 0.5 to 10 g(O) / 100 g(F0), more preferably in the range of 0.5 to 5 g(O) / 100 g(F0), and more preferably in the range of 0.5 to 2 g(O) / 100 g(F0), as determined as described in Reference Example 4.

[0163] The process according to any one of Embodiments 1 to 3, wherein the pyrolysis oil according to 4.(i) has a total acid number (TAN) in the range of 0.5 to 60 Mg KOH / g(F0), preferably in the range of 1 to 40 Mg KOH / g(F0), and preferably in the range of 3 to 20 Mg KOH / g(F0), as determined as described in Reference Example 3.

[0164] The pyrolysis oil according to 5.(i) has a total chlorine content in the range of 30 to 3,000 WPPM (particles by weight), preferably 30 to 500 WPPM, and more preferably 30 to 300 WPPM, as determined as described in Reference Example 1.1. The process according to any one of Embodiments 1 to 4, wherein the pyrolysis oil produced by (i) has a chloride content in the range of at most 40 WPPM, more preferably 0 to 30 WPPM, as determined as described in Reference Example 1.2.

[0165] The process according to any one of Embodiments 1 to 5, wherein the pyrolysis oil according to 6.(i) has a nitrogen content in the range of 50 to 20,000 WPPM (ppm by weight), preferably 50 to 5,000 WPPM, more preferably 100 to 4,000 WPPM, as determined as described in Reference Example 2.

[0166] 7.(ii.2) is, (ii.2.1) Water Z E The process of introducing it into UM1, (ii.2.2) A step of bringing F0 into contact with water, preferably mixing it, and adding it to UM1 to obtain a mixture PM1 containing water and pyrolysis oil, (ii.2.3) B is introduced into UM1, and B is brought into contact with the mixture PM1 obtained in (ii.2.2), preferably mixed, and introduced into UM1, and the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of is in the range of 7.5 to 11, preferably in the range of 8 to 10, and the process It includes, preferably (ii.2), (ii.2.1) Water Z E The process of introducing it into UM1, (ii.2.2) Bring F0 into contact with water, preferably mixed, Z EA step of placing into [a container] to obtain a mixture PM1 containing water and pyrolysis oil, wherein the aqueous phase of PM1 preferably has a pH value of pH(PM1) measured by a pH sensor in UM1. (ii.2.3) Contact B with M1 obtained in (ii.2.2), preferably mix them, and introduce B into UM1 by placing them into UM1, thereby adjusting the pH of the aqueous phase of PM1 to obtain an aqueous phase P A (1) and an organic phase P O A step of obtaining a mixture M1 containing (1), wherein the aqueous phase P A (1) has a pH > pH(PM1), and P A (1) has a pH in the range of 7.5 to 11, preferably in the range of 8 to 10. A process according to any one of Embodiments 1 to 6, including

[0167] 8. (ii.2) is (ii.2.1’) A step of mixing water and B to obtain a mixture M0 of water and B having a pH(M0) in the range of 12 to 14. (ii.2.2’) Introduce M0 obtained according to (ii.2.1’) into UM1, contact F0 with M0, more preferably mix them, to obtain an aqueous phase P [[ID=二十一]]<00の00189> (1) and an organic phase P O A step of obtaining a mixture M1 containing (1), wherein the aqueous phase P A (1) has a pH in the range of 7.5 to 11, preferably in the range of 8 to 10. A process according to any one of Embodiments 1 to 6, including

[0168] 9. The process according to any one of Embodiments 1 to 8, wherein the extraction unit UM1 is one or more of a stirring container, a mixing pump, and a static mixer, preferably a stirring container.

[0169] 10. The step of contacting, preferably mixing, according to (ii.2) is carried out at a temperature T1 in the range of 10 to 95 °C, preferably in the range of 15 to 85 °C, more preferably in the range of 20 to 80 °C. The process according to any one of Embodiments 1 to 9.

[0170] 11. The process according to any one of Embodiments 1 to 10, wherein the base B is one or more of alkali metal compounds, alkaline earth metal compounds, and ammonia, preferably B is 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, and more preferably potassium hydroxide.

[0171] The process according to any one of Embodiments 1 to 11, wherein the water used in 12.(ii) is desalinated water.

[0172] 13. The process according to any one of embodiments 1 to 12, wherein the liquid-liquid separation unit US1 is one or more of a hydrocyclone, a settler tank, and a centrifuge, preferably a decanter, a hydrocyclone, a settler tank, or a centrifuge, more preferably a settler tank.

[0173] The process according to any one of Embodiments 1 to 13, wherein the separation in US1 according to 14.(ii.3) is carried out at a temperature in the range of 10 to 95°C, preferably in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

[0174] Before passing M1 through US1 in accordance with 15.(ii.3), this process is performed, The process according to any one of embodiments 1 to 14, further comprising passing M1 through a solid-liquid separation unit SLS1 for removing solids in M1, if present.

[0175] 16. The process according to Embodiment 15, wherein the solid-liquid separation unit SLS1 is one or more of a filter and a centrifuge.

[0176] 17. Separation unit USA1, preferably in the sedimentation tank, P obtained according to (ii.3) A Flow F including (1) A (1) A process to obtain an aqueous flow SA1 containing water The process according to any one of embodiments 1 to 16, further including the process described above.

[0177] The process according to any one of Embodiments 1 to 17, wherein no organic solvent is used in 18.(ii).

[0178] 19. In US1, P A (1) and P O The process according to any one of Embodiments 1 to 18, further comprising the step of purging the precipitate from US1 if a precipitate is formed at the interface with (1).

[0179] 20. (iii) is, (iii.1) F1 to Z W The process involves introducing the material into the cleaning unit UM2 provided therein, (iii.2) F1 is brought into contact with water in UM2 at a temperature T2 in the range of 10 to 95°C, and the aqueous phase P A (2) and organic phase P O (2) A step to obtain a mixture M2 comprising the aqueous phase P of M2 A (2) The pH is in the range of 7.5 to 11, P A (2) PH <P A (1) The pH of the process, The mixture M2 obtained according to (iii.3)(iii.2) is Z W It is provided and passes through the liquid-liquid separation unit US2 located downstream of UM2, P A Flow F including (2) A (2) and P, which is a refined pyrolysis oil. O (2) A process to obtain flow F2 including (2) A process according to any one of embodiments 1 to 19, including the process described above.

[0180] 21. The process according to Embodiment 20, wherein the washing unit UM2 is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel.

[0181] The process according to Embodiment 20 or 21, wherein the weight ratio of water to F1 is in the range of 0.05:1 to 2:1, preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, more preferably in the range of 0.1:1 to 0.5:1, or more preferably in the range of 0.8:1 to 1.2:1.

[0182] 23. The process according to any one of embodiments 20 to 22, wherein the liquid-liquid separation unit US2 is one or more of a hydrocyclone, a sedimentation tank, and a centrifuge, preferably a hydrocyclone, a sedimentation tank, or a centrifuge, more preferably a sedimentation tank or a centrifuge.

[0183] The process according to any one of embodiments 20 to 23, wherein the separation in US2 according to 24.(iii.3) is carried out at a temperature in the range of 10 to 85°C, preferably in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

[0184] Before passing M2 through US2 according to 25.(iii.3), this process, The process according to any one of embodiments 20 to 24, further comprising passing M2 through a solid-liquid separation unit SLS2 to remove solids in M2, if present.

[0185] 26. The process according to Embodiment 25, wherein the solid-liquid separation unit SLS2 is one or more of a filter and a centrifuge.

[0186] 27. The process according to any one of embodiments 20 to 24, wherein no separation unit is located between UM2 and US2.

[0187] 28.(iii) is, (iii.1') F1 to ZW The step of introducing into the extraction column UM+US provided therein, and (iii.2’) The step of introducing water into UM+US, and (iii.3’) Contacting F1 with water at a temperature T2’ in the range of 10 to 95 °C in UM+US to obtain a water phase P A (2)-containing stream F A (2) is obtained (aqueous phase P of M2 A (2) has a pH in the range of 7.5 to 11, and P A (2) has a pH < P A (1)’s pH), and the step of obtaining a stream F2 containing purified pyrolysis oil A process according to any one of Embodiments 1 to 19, including

[0188] 29. According to (iii.3’), the weight ratio of water to F1 is in the range of 0.05:1 to 2:1, preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, more preferably in the range of 0.1:1 to 0.5:1, or more preferably in the range of 0.8:1 to 1.2:1, the process according to Embodiment 28.

[0189] 30. Recycling at least a part of the water contained in F A (2) in (ii.2) and / or (iii.2), or Recycling at least a part of the water contained in F A (2) obtained according to (iii.3’) in (ii.2) and / or (iii.2’), and / or Recycling at least a part of the water contained in F A (1) obtained according to (ii.3) in (ii.2) A process according to any one of Embodiments 20 to 29, further including

[0190] 31. In (iii), no organic solvent is used, the process according to any one of Embodiments 1 to 30.

[0191] The process according to any one of Embodiments 1 to 31, wherein the flow F2 containing the refined pyrolysis oil obtained according to 32.(iii) has a TAN lower than the total acid number (TAN) of the pyrolysis oil provided in (i).

[0192] The process according to Embodiment 32, wherein the flow F2 containing the refined pyrolysis oil obtained according to 33.(iii) has a TAN in the range of 0 to 20 Mg KOH / g(F2), more preferably in the range of 0 to 10 Mg KOH / g(F2), and more preferably in the range of 0 to 4 Mg KOH / g(F2), as determined as described in Reference Example 3.

[0193] The process according to any one of Embodiments 1 to 33, wherein the flow F2 containing the refined pyrolysis oil obtained according to 34.(iii) has an oxygen content less than or equal to, more preferably less than, the oxygen content of the pyrolysis oil provided in (i).

[0194] 35. The process according to Embodiment 34, wherein the flow F2 containing the refined pyrolysis oil has an oxygen content in the range of 0 to 2 g(O) / 100 g(F2), as determined as described in Reference Example 4.

[0195] 36.(iv)(iii) At least a portion of the flow F2 obtained according to Z W (iv) further includes subjecting to one or more subsequent washes in (iv.1) Depending on the case, at least a portion of F2 obtained according to (iii), preferably F2, Z W It is equipped and introduced into the washing unit UM3 located downstream of US2, At least a portion of F2, preferably F2, is brought into contact with water in UM3 at a temperature T3 ranging from 10 to 95°C, forming an aqueous phase P A (3) and organic phase P O (3) is included and ranges from 7.5 to 11, P A (3) PH <P A (1) A mixture M3 with the pH of (1) is obtained. Z WIn the liquid-liquid separation unit US3 located downstream of UM3, the mixture M3 is passed through P A Flow F including (3) A (3) and P, which is a refined pyrolysis oil. O (3) A process to obtain flow F3 including, At least a portion of F2 obtained according to (iv.2)(iii), preferably F2, or at least a portion of F3 obtained according to (iv.1), preferably F3, Z W The process involves preparing for and introducing the solution into the washing unit UM4 located downstream of US3, (iv.3) At least a portion of F2, preferably F2, or at least a portion of F3, preferably F3, is brought into contact with water in UM4 at a temperature T4 in the range of 10 to 95°C, forming an aqueous phase P A (4) and organic phase P O (4) A step to obtain a mixture M4 containing the aqueous phase P of M4 A (4) The pH is in the range of 7.5 to 11, P A (4) PH <P A (1) The pH of the process, The mixture M4 obtained according to (iv.4)(iv.3) is Z W It is provided and passes through the liquid-liquid separation unit US4 located downstream of UM4, P A Flow F including (4) A (4) and P, which is a refined pyrolysis oil. O (4) A process to obtain flow F4 including (4) The process of any one of embodiments 1 to 35, including, insofar as embodiment 36 depends on any one of embodiments 20 to 27.

[0196] 37. A step of introducing F2 containing the pyrolysis oil obtained according to (v)(iii), and optionally F4 obtained according to (iv), into at least one storage unit SU, and storing the pyrolysis oil in the SU. The process according to any one of embodiments 1 to 36, further including the following.

[0197] 38. The process according to embodiment 37, wherein the storage unit SU is a storage tank, preferably made of one or more of steel and stainless steel, more preferably carbon steel and stainless steel.

[0198] 39. The process according to any one of Embodiments 1 to 38, further comprising one or more of the following steps: a dechlorination step, a hydrogenation step, a hydrotreatment step, a steam decomposition step, a hydrocracking step, a distillation step, a stripping step, and an aqueous extraction step.

[0199] 40. A process according to any one of embodiments 1 to 39, which is a continuous or semi-continuous process.

[0200] 41. A unit for carrying out a process for refining pyrolysis oil according to any one of Embodiments 1 to 40, - At least one extraction zone Z comprising an extraction unit UM1 and a liquid-liquid separation unit US1 E Therefore, UM1 is located upstream of US1, in extraction zone Z. E and, -F0 to Z E An entry point for introducing it, -Z E An exit means for removing F1 from, - An entry point for introducing F0 into UM1, - An exit means for removing M1 from UM1, - An entry point for introducing M1 into US1, - An exit strategy from removing F1 from US1, -Z E At least one washing zone Z located downstream W and, -F1 to Z W An entry point for introducing it, -Z W An exit means for removing F2 from and A unit equipped with [the necessary components].

[0201] 42.US1 is P A (1) and PO The unit according to embodiment 41, comprising means for purging an optional precipitate formed at the interface with (1).

[0202] 43.Z W but, - Cleaning unit UM2, -Liquid-liquid separation unit US2, wherein UM2 is located upstream of US2, - An entry point for introducing F1 into UM2, - An inlet for introducing water into UM2, - An exit means for removing M2 from UM2, - An entry point for introducing US2 to M2, - An exit strategy from removing F2 from US2 The unit according to embodiment 41 or 42, comprising:

[0203] 44.Z W However, the system further comprises a washing unit UM4, preferably a mixing unit and a liquid-liquid separation unit US4, wherein UM4 is located downstream of US2, and US4 is located downstream of UM4. Depending on the case, Z W The unit according to Embodiment 43, further comprising a washing unit UM3, preferably a mixing unit and a liquid-liquid separation unit US3, wherein UM3 is located downstream of US2 and upstream of UM4, and US3 is located downstream of UM3 and upstream of UM4.

[0204] 45.Z W but, - Extraction column UM+US and, - An entry point for introducing F1 into UM+US, - An inlet for introducing water into UM+US, - An exit method from removing F2 from UM+US The unit according to embodiment 41 or 42, comprising:

[0205] 46. ​​The unit according to any one of embodiments 41 to 45, further comprising one or more of the following: a storage tank, a cracking zone, an adsorption zone, a dechlorination zone, a hydrogenation zone, a hydrogenation treatment zone, a stripping zone, and a distillation zone.

[0206] 47. A step of obtaining a refined pyrolysis oil, monomer, polymer, or polymer product using the unit described in any one of embodiments 41 to 46. A process that includes this.

[0207] 48. Preferably, - A process that can be obtained by any one of Embodiments 1 to 40, or a process that converts the resulting flow F2, or a chemical substance that can be obtained by any one of Embodiments 1 to 40, to obtain a monomer, polymer, or polymer product. A process comprising the steps described in any one of embodiments 1 to 40, further including the steps described in any one of embodiments 1 to 40.

[0208] 49. The polymer or polymer product is a granular material, strand, rod, plate, pipe, foil, layer, film, sheet, fiber, filament, coating, extruded and / or molded article, flexible foam, semi-rigid foam and / or rigid foam. The process described in Embodiments 1 to 40 and / or any one of 47 or 48.

[0209] 50. The monomer is a diol or polyol; preferably butanediol; aldehyde; preferably formaldehyde; diisocyanate or polyisocyanate; preferably methylenediphenyl diisocyanate (MDI), polymerizable methylenediphenyl diisocyanate (PMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI), or isophorone diisocyanate (IPDI); amide; preferably caprolactam; alkene; preferably styrene, ethene, and norbornene; alkyne, (di)ester; preferably methyl methacrylate; monoacid or diacid; preferably adipic acid or terephthalic acid; diamine; preferably hexamethylenediamine, nonanediamine, or sulfone; preferably 4,4'-dichlorodiphenyl sulfone. The process described in any one of embodiments 1 to 40 and / or 47 to 49.

[0210] 51. The polymer is polyamide (PA); preferably PA6 and PA66; polyisocyanate polyaddition product; preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), polyacrylonitrile butadiene styrene (ABS), polystyrene acrylonitrile (SAN), polyacrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (TEFlON), thermoplastic polyurethane (TPU), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis-1,4-isoprene), poly(TRANS-1,4-isoprene), polyoxymethylene ( Polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate copolymer (PBAT), polyester (PES), polyethersulfone (PESU), polyhydroxyalkanoate (PHA), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyetheretherketone (PEEK), poly(p-phenylene oxide) (PPO), poly(p-phenylene ether) (PPE); and copolymers and mixtures thereof, and / or polymer products containing them. The process described in any one of embodiments 1 to 40 and / or 47 to 50.

[0211] 52. Polymers and / or polymer products, - Automotive parts, preferably cylinder head covers, engine covers, housings for intake refrigerants, intake refrigerant flaps, intake pipes, intake manifolds, connectors, gear wheels, fan wheels, coolant boxes, housings or housing components for heat exchangers, coolant coolers, intake refrigerants, thermostats, water pumps, radiators, fastening components or parts of battery systems for electric transport, dashboards, steering column switches, seats, headrests, center consoles, transmission components, door modules, automotive exteriors for A, B, C or D pillar covers, spoilers, door handles, exterior mirrors, windscreen wipers, windscreen wiper protective housings, decorative grilles, cover strips, roof rails, window frames, sunroof frames, antenna panels, headlights and taillights, engine covers, cylinder head covers, intake manifolds, airbags, or cushions; - Cloth, preferably a shirt, trousers, pullover, boots, shoes, soles, tights, or jacket; - Electrical components, preferably passive or active electrical or electronic components, printed circuit boards, printed circuit board housing components, foils, lines, switches, plugs, sockets, distributors, relays, resistors, capacitors, inductors, bobbins, lamps, diodes, LEDs, transistors, connectors, regulators, integrated circuits (ICs), processors, controllers, memory, sensors, connectors, microswitches, microbuttons, semiconductors, reflector housings for light-emitting diodes (LEDs), fasteners, spacers, bolts, strips, slide-in guides, screws, nuts, film hinges, snap hooks (snap-ins), or spring tongues for electrical or electronic components; -Consumer products and / or pharmaceuticals, preferably tennis strings, climbing ropes, bristle, brushes, artificial grass, 3D printing filaments, grass trimmers, zippers, hook-and-loop fasteners, paper machine clothing, extruded coatings, fishing lines, fishing nets, offshore lines and ropes, vials, syringes, ampoules, bottles, sliding elements, spindle nuts, chain conveyors, plain bearings, rollers, wheels, gears, rollers, ring gears, screws and spring dampers, hoses, pipelines, cable sheathing, sockets, switches, cable ties, fan wheels, carpets, cosmetic boxes or bottles, mattresses, cushions or insulation; and / or - Packaging for the food industry; preferably single-layer or multi-layer inflation film, cast film (single-layer or multi-layer), biaxially oriented film, laminate film The process described in any one of embodiments 1 to 40 and / or 47 to 51, which is either or a part thereof.

[0212] 53. The content of pyrolysis oil in the flow F0 in the refined pyrolysis oil, monomer, polymer and / or polymer product is 1% by weight or more, preferably 2% by weight or more, more preferably 5% by weight or more, more preferably 15% by weight or more, more preferably 30% by weight or more, more preferably 40% by weight or more, more preferably 60% by weight or more, more preferably 80% by weight or more, more preferably 90% by weight or more, more preferably 95% by weight or more, and / or The content of pyrolysis oil in the flow F0 in the refined pyrolysis oil, monomer, polymer and / or polymer product is 100% by weight or less, preferably 95% by weight or less, more preferably 90% by weight or less, more preferably 50% by weight or less, more preferably 25% by weight or less, and more preferably 10% by weight or less. Preferably, the content is determined based on an identity retention and / or separation and / or mass balance and / or book-and-claims chain of custody model, preferably based on mass balance, preferably based on the International Sustainable Carbon Certification (ISCC) standard, according to any one of Embodiments 1 to 40 and / or 47 to 52.

[0213] 54. A refined pyrolysis oil that can be obtained or is obtained by the process described in any one of Embodiments 1 to 40.

[0214] It should be explicitly noted that the above set of embodiments represents a well-structured portion of a general description directed toward preferred embodiments of the present invention, and therefore adequately supports, but does not represent, the claims of the present invention.

[0215] In the context of the present invention, the term “precipitate” refers to an electrostatic, solid, or surface-activated stabilizing layer containing an aqueous phase and an organic phase, which most commonly accumulates at the water / organic interface in precipitating agents in solvent extraction processes known in the art.

[0216] In the context of the present invention, the phrase "X is one or more of A, B, and C" should be understood as disclosing that X is either A, B, or C, or A and B, or A and C, or B and C, or A, B, and C. In this regard, those skilled in the art can translate the above abstract terms into concrete examples, for example, X is a chemical element and A, B, and C are specific elements, e.g., Li, Na, and K, or X is a temperature and A, B, and C are specific temperatures, e.g., 10°C, 20°C, and 30°C. In this regard, it should be noted that it is possible to extend the above terms to less specific realizations of the features, for example, "X is one or more of A and B" to disclose that X is either A, or B, or A and B, or for more specific realizations of the features, for example, "X is one or more of A, B, C, and D" to disclose 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.

[0217] A conversion step to obtain a monomer, polymer, or polymer product may include one or more synthesis steps, which can be carried out by conventional synthesis and techniques well known to those skilled in the art. Regardless of whether a person skilled in the art can evaluate the novelty and inventive step of an independent claim, a person skilled in the art to carry out a conversion step is from the art of the thermal decomposition, gasification, remonomerization, depolymerization and / or synthesis and / or manufacture of monomers, polymers and polymer compounds, and further processing thereof (e.g., extrusion molding, injection molding). Examples of conversion processes are found in: "Industrial Organic Chemistry", Vol. 3, Wiley-VCH, 1997; ISBN: 978-3-527-28838-0; "Kunststoffhandbuch", Vol. 11 divided into 17 volumes, Carl Hanser Verlag, especially Vol. 6, "Polyamide", 1st edition, 1966; Vol. 7, "Polyurethane", 3rd edition, 1993; and Vol. 8, "Polyester", 1st edition, 1973; "Industrial Organic Chemistry", Vol. 3, 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),WO2006034800 (A1), EP1529792(A1), WO2006042674(A1), EP0364854(A2), US5506275(A), EP0897402(A1 These are described in WO2015082316(A1), WO2021021855(A1), WO2021126938(A1), WO2021021902(A1), WO2021092311(A1), WO2008155271(A1), and WO2013139827(A1), which are incorporated herein by reference, respectively.

[0218] The present invention is further illustrated by the following embodiments. [Examples]

[0219] Examples Reference Example 1.1 Measurement of Total Chlorine Content (WPPM) Before analysis, the samples are filtered through a 0.45 μM syringe filter. The chlorine content is determined by combustion of each sample at 1050°C. The resulting combustion gas, i.e., hydrogen chloride, is then introduced into a cell where coulometric titration is performed.

[0220] Reference Example 1.2 Measurement of Chloride Content (WPPM) Before analysis, the sample was filtered through a 0.45 μM syringe filter. Chloride content was determined by ion chromatography. Instrument: Ion Chromatograph 850 Professional (METROHM) (Pre-column: METROSEP A SUPP 4 / 5 S-GUARD and analytical column: METROSEP A SUPP 5 250 / 4; Flow rate: 0.7 ML / min; Column temperature: 30°C; Detector temperature: 40°C; Injection volume: 25 μL; Suppressor: MSM HC rotor A). Eluents used were: 3.2 MMO1 / L NA2CO3; 1.0 MMO1 / L NAHCO3; and inhibitor / regenerator: 50 MMO1 / L sulfuric acid.

[0221] Sample preparation: 0.2 g to 0.4 g of sample was weighed and dissolved in 10 ml of toluene. 10 ml of deionized water was added for sample extraction. After centrifugation, the aqueous phase was extracted and analyzed. Recovery rates were confirmed by adding a 20 μg / L chloride standard solution (corresponding to the limit value of 1 Mg / kg chloride in the sample) to samples with concentrations below the method's limit.

[0222] Reference Example 2: Measurement of N content (WPPM) The nitrogen content is determined by combustion of each sample at 1000°C. NO contained in the resulting combustion gas reacts with ozone to form NO2*. The relaxation of the excited nitrogen species is detected by a chemiluminescence detector according to ASTM D4629(N). The calibration range is 0.5 WPPM to 50 WPPM. Higher concentration samples are diluted with xylene to bring them within the calibration range.

[0223] Reference Example 3: Measurement of Total Acid Number (TAN) The total acid value was determined by titration with KOH according to ASTM D3242.

[0224] Reference Example 4: Measurement of Oxygen Content (O Content) (by weight %) Samples (1–10 Mg) were thermally decomposed / reduced in a reducing gas atmosphere over a soot contact, thereby converting oxygen to carbon monoxide (CO). Carbon monoxide was detected and quantified by IR spectroscopy. The analyzer used was the RAPiD OXY CUBE®, an analyzer model from ElEMENTAR.

[0225] Reference Example 5: Corrosion Test Two corrosion test specimens of steel 1.0425 (DIN EN 10028-2) were stored in pyrolysis oil tested at 60°C under a nitrogen atmosphere. Every 7 days, the samples were washed again with water, xylene, and water, dried, and weighed. The culture medium was replaced with fresh pyrolysis oil, and the samples were returned. After 4 cycles (28 days), the mean linear corrosion rate* was calculated, and the specimens were examined. The surface of the corrosion test specimens was examined using a binocular microscope at 10x to 20x magnification according to DIN 50905 to detect various corrosion phenomena, the frequency, degree, and distribution of localized corrosion, as well as discoloration, scale formation, or corrosion products on the specimen surface. The depth of localized corrosion, such as shallow pit corrosion, was measured by optical focusing with an optical microscope. v l : Mean line corrosion rate [MM / year] DM: Weight loss [g] F: Surface of the test specimen [CM 2 ] R: Density of material [g / cm³] 3 ] T: Exam time [days]

[0226] Reference Example 6: Measurement of FE, SN, and Zn content (WPPM) Aliquots of approximately 0.35–0.40 g of the sample were weighed and transferred to an automated acid digestion system. The digestion process included the following steps: - Cracking of samples with a mixture of H2SO4 and HNO3 at approximately 320°C - Complete digestion of organic residues by a mixture of H2SO4, HNO3, H2O2, and HClO4 at approximately 160°C. - Removal of excess acid by almost complete evaporation to dryness. - Dissolution of digested residue in 5% (v / v) hydrochloric acid by heating to the boiling point.

[0227] The digestion process was carried out in two separate steps. A blank sample was prepared using a similar method.

[0228] FE, SN, and Zn content measurements were determined in the digested solution via inductively coupled plasma atomic emission spectroscopy (ICP-OES) with external calibration and blank subtraction. The results were averages of both replicas.

[0229] Example 1: Process for refining pyrolysis oil according to the present invention Total acid number (TAN) of approximately 8.5 Mg KOH / g, total chlorine content of 24 WPPM, chloride content of <5 WPPM, nitrogen content of 0.5 wt% based on the weight of the pyrolysis oil, and oxygen content of 1 wt% based on the weight of the pyrolysis oil, 916 kg / M 3 A feed stream F0 containing pyrolysis oil with density and viscosity of 6.4 MPAS was subjected to extraction with NaOH (1.1) or KOH (1.2) and (1.3) at T=30°C and pH 10. To do so, F0 was introduced into a 1.3 L stirred glass container. Demineralized water was then added to the container (phase ratio v(demineralized water / pyrolysis oil) = 0.3 kg / kg) to form a mixture. The pH of the aqueous phase of the mixture was adjusted to 10 using 10% NaOH (1.1) or KOH (1.2 and 1.3). The resulting mixtures were mixed for 15 minutes. For the mixture with NaOH, the mixture was transferred to a centrifuge. For the mixture with KOH, the mixture was allowed to settle in a 1.3 L glass container for 5 minutes (1.2) and 7 minutes (1.3). Thus, after settling, the aqueous phase was separated from the organic (oil) phase. The organic phase was analyzed.

[0230] After separating the aqueous phase in the neutralization process, demineralized water was further added to the organic phase to remove residual salt / caustic substances (entrainment). Demineralized water was added at a phase ratio v(desalinated water / organic phase) = 1 kg / kg. The resulting aqueous / organic (oil) phase of the mixture was introduced into a settler (liquid-liquid separation unit). After sedimentation, the aqueous phase was separated from the organic phase, and the washed organic phase was analyzed. Different sedimentation times were applied depending on the sample: 8 minutes for 1.1, 6 minutes for 1.2, and 2.5 minutes for 1.3. The results are listed in Table 1 below.

[0231] [Table 1]

[0232] As can be seen from Table 1, extraction and washing allows for the purification of pyrolysis oil by reducing its TAN, oxygen content, and N and Cl content.

[0233] Corrosion test: Corrosion tests were performed using pyrolysis oil F0 and the refined pyrolysis oils obtained after washing samples 1.1, 1.2, and 1.3, as described in Reference Example 5. The results are detailed in Tables 2 to 4 below.

[0234] [Table 2]

[0235] As can be seen from Table 2, the pyrolysis oil before the refining treatment according to the present invention was corrosive. Localized corrosion and pitting corrosion are unacceptable.

[0236] [Table 3]

[0237] As can be seen from Table 3, the pyrolysis oil refined according to the present invention using NAOH significantly reduces corrosion, i.e., only average linear corrosion vl and sporadic rust marks (superficial) exceeding 99%. Therefore, in contrast to the comparative example, there is no pitting or localized corrosion, which demonstrates a clear improvement. The refined pyrolysis oil does not affect the technical stability of the steel material (less than 0.1 MM / y vl in a combination without pitting or localized corrosion).

[0238] [Table 4]

[0239] As can be seen from Table 4, the pyrolysis oil refined according to the present invention using KOH significantly reduces corrosion, i.e., only about 80% average linear corrosion vl and sporadic rust marks (superficial). Therefore, in contrast to the comparative example, there is no pitting or localized corrosion, which demonstrates a clear improvement. The refined pyrolysis oil does not affect the technical stability of the steel material.

[0240] Therefore, while the pyrolysis oil before refining according to the present invention was corrosive, it has been demonstrated that the refined pyrolysis oil (TAN<1) significantly reduces corrosion without affecting the technical stability of the steel material.

[0241] Reference Example 7: Process for refining pyrolysis oil not according to the present invention - Corrosion test Further processes have been carried out to purify the pyrolysis oil in order to identify the optimal conditions for purification. A feed stream F0 containing pyrolysis oil, as in Example 1, was subjected to extraction with KOH at pH 7 at T=50°C. To do so, F0 was introduced into a 1.3 L stirred glass vessel. Demineralized water was then added to the vessel (phase ratio v(water / pyrolysis oil) = 0.5 kg / kg) to form a mixture. The pH of the aqueous phase of the mixture was adjusted to 7.2 with 25 wt% KOH. The resulting mixture was mixed for 15 minutes. After sedimentation (2 minutes), the obtained aqueous phase was separated from the organic phase. The organic phase was analyzed.

[0242] The washing process was performed again. Demineralized water was added to the organic phase at a ratio v(demineralized water / organic phase) = 0.5 kg / kg to remove salt and caustic entrainment from the pyrolysis oil. The results are listed in Table 5 below.

[0243] [Table 5]

[0244] As can be seen from Table 5, the decrease in TAN was much smaller at PH7.

[0245] Corrosion test: A corrosion test was performed using pyrolysis oil F0 (see Table 2 above) and refined pyrolysis oil obtained independently of the present invention (with different pH levels), as described in Reference Example 5. The results are detailed in Table 6 below.

[0246] [Table 6]

[0247] As can be seen from Table 6, pyrolysis oil refined with KOH at pH 7, without following the present invention, reduces mean line corrosion vl. However, pyrolysis oil is more corrosive than the refined pyrolysis oil obtained according to the process of the present invention (see Tables 3 and 4 above). Even if vl is reduced, the presence of localized corrosion and pitting corrosion is unacceptable.

[0248] Example 2 Process for refining pyrolysis oil according to the present invention Total acid number (TAN) of 15.9 Mg KOH / g, total FE content of 15 WPPM, SN content of 3 WPPM, Zn content of 5 WPPM based on the weight of the pyrolysis oil, 863 kg / M 3A feed stream F0 containing pyrolysis oil with density and viscosity of 1.7 MPAS was subjected to extraction with NaOH at T=25°C and pH 10. To do so, F0 was introduced into a 1.3 L stirring glass container. Demineralized water was then added to the container (phase ratio v(demineralized water / pyrolysis oil) = 0.5 kg / kg) to form a mixture. The pH of the aqueous phase of the mixture was adjusted to 10 with 25% NaOH. The resulting mixture was mixed for 15 minutes. For the mixture with NaOH, the mixture was transferred to a centrifuge. In this way, the aqueous phase was separated from the organic (oil) phase after sedimentation. The organic phase was analyzed.

[0249] After separating the aqueous phase in the neutralization process, demineralized water was further added to the organic phase to remove residual salt / caustic substances (entrainment). Demineralized water was added at a phase ratio v(desalinated water / organic phase) = 1 kg / kg. The resulting aqueous / organic (oil) phase of the mixture was introduced into a settler (liquid-liquid separation unit). After sedimentation, the aqueous phase was separated from the organic phase, and the washed organic phase was analyzed. The results are listed in Table 7 below.

[0250] [Table 7]

[0251] As can be seen from Table 7, extraction (neutralization) makes it possible to purify the pyrolysis oil by reducing its TAN, FE, SN, and Zn content.

[0252] Comparative Example 1: A process for refining pyrolysis oil not according to the present invention. A feed stream F0 containing pyrolysis oil with a total acid number (TAN) of 7 Mg KOH / g was subjected to a first washing step with demineralized water, and the mixture was placed in a 250 ml glass bottle with a phase ratio of v (demineralized water / pyrolysis oil (F0)) = 1 kg / kg. The mixture was shaken. The pH of the aqueous phase of the mixture was 4.3. The resulting water / organic phase (oil) of the mixture was introduced into a centrifuge. In this way, the aqueous phase was separated from the organic (oil) phase.

[0253] After separating the aqueous phase from the organic phase, demineralized water was further added to the organic phase for a second washing step. The demineralized water was added at a phase ratio v(desalinated water / organic phase) = 1 kg / kg. The resulting water / organic phase (oil) mixture was introduced into a centrifuge. The aqueous phase was then separated from the organic phase. Finally, a third washing step was performed to separate the aqueous phase from the organic phase using a centrifuge, and the washed organic phase was analyzed. The results are listed in Table 3 below.

[0254] [Table 8]

[0255] As can be seen from Table 8, the cleaning process is not sufficient to reduce the TAN count.

[0256] Reference Example 8: Testing different bases In this example, the pyrolysis oils (each of which has a total acid number (TAN) of approximately 8.5 Mg KOH / g, a total chlorine content of 24 WPPM, a chloride content of <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, 916 kg / M 3 The oils (having a density and viscosity of 6.4 MPAS) were extracted with NaOH or KOH in a centrifuge glass tube under the conditions detailed in Table 9. After extraction, phase separation of these oils was observed (see Table 9).

[0257] [Table 9]

[0258] As can be seen from Table 9, when NaOH is used for the extraction of pyrolysis oil at a pH of approximately 10, solids are formed that do not allow for phase separation between the aqueous and oil phases due to the gravitational field. Further centrifugation steps were required to separate the solids, aqueous phase, and oil phase after extraction. As the pH during extraction decreased, less solid was formed, and the phase separation between the aqueous and oil phases became clearly visible—making it easier to separate the aqueous and oil phases after extraction. Furthermore, when KOH was used for the extraction of pyrolysis oil, even less solid was formed at a pH of approximately 10. While we do not wish to be bound by any theory, using NaOH for the extraction of pyrolysis oil may result in the formation of sodium soaps (sodium salts of fatty acids), which are mostly solids and therefore hinder the phase separation between the aqueous and oil phases after extraction, in contrast to potassium soaps (potassium salts of fatty acids), which are mostly liquids and therefore do not hinder the phase separation between the aqueous and oil phases after extraction. Therefore, KOH may be chosen over NaOH to avoid these drawbacks.

[0259] References - U.S. Patent Application Publication No. 2021 / 0277324 - International Publication No. 2014 / 165859 Pamphlet - International Publication No. 2020 / 178599 brochure

Claims

1. A process for refining pyrolysis oil, (i) A step of providing a flow F0 containing the pyrolysis oil, (ii) Take the flow F0 provided in (i) into at least one extraction zone Z E A step of subjecting to extraction to obtain a flow F1 containing the extracted pyrolysis oil, (ii.1) Set F0 to Z E The process of introducing the contents into the extraction unit UM1 provided therein, (ii.2) F0 is brought into contact with water and base B in UM1 at a temperature T1 in the range of 10 to 200°C, and aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of the process is in the range of 7.5 to 11. The mixture M1 obtained according to (ii.3) (ii.2) is passed through Z E which is provided in and located downstream of UM1 to a liquid-liquid separation unit US1, and P A a stream F containing (1) A (1) and the extracted pyrolysis oil P O to obtain a stream F1 containing (1). (ii.4) Z E (ii) includes the step of removing F1 from, (iii) The flow F1 provided in (ii) is Z E At least one washing zone Z located downstream W The process involves subjecting the mixture to cleaning to obtain a flow F2 containing the refined pyrolysis oil. A process that includes this.

2. (ii.2) However, (ii.2.1) Water Z E The process of introducing it into UM1, (ii.2.2) A step of bringing F0 into contact with water in UM1, preferably by mixing, to obtain a mixture PM1 containing water and the pyrolysis oil, (ii.2.3) B is introduced into UM1, and B is brought into contact with the mixture PM1 obtained in (ii.2.2) in UM1, preferably mixed to form the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of the process is in the range of 7.5 to 11, preferably in the range of 8 to 10. It includes, preferably (ii.2), (ii.2.1) Water Z E The process of introducing it into UM1, (ii.2.2) A step of bringing F0 into contact with water in UM1, more preferably mixing it to obtain a mixture PM1 containing water and the pyrolysis oil, wherein the aqueous phase of PM1 has a pH (PM1) measured by a pH sensor in UM1, more preferably (ii.2.3) By introducing B into UM1 by contacting it with M1 obtained in (ii.2.2) in UM1, and preferably by mixing them, the pH of the aqueous phase of PM1 is adjusted, and the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) PH > PH(PM1), and P A (1) The pH of the process is in the range of 7.5 to 11, more preferably in the range of 8 to 10. The process according to claim 1, including the process described in claim 1.

3. (ii.2) However, (ii.2.1') ​​A step of mixing water and B to obtain a mixture M0 of water and B having a pH (M0) in the range of 12 to 14, The M0 obtained according to (ii.2.2') and (ii.2.1') ​​is introduced into UM1, and F0 is brought into contact with M0 in UM1, more preferably mixed, to form the aqueous phase P A (1) and organic phase P O A step to obtain a mixture M1 containing (1), wherein the aqueous phase P of M1 A (1) The pH of the process is in the range of 7.5 to 11, preferably in the range of 8 to 10. The process according to claim 1, including the process described in claim 1.

4. The process according to any one of claims 1 to 3, wherein the extraction unit UM1 is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel.

5. The process according to any one of claims 1 to 4, wherein the step of contacting, preferably mixing, in accordance with (ii.2) is performed at a temperature T1 in the range of 10 to 95°C, preferably in the range of 15 to 85°C, more preferably in the range of 20 to 80°C.

6. The process according to any one of claims 1 to 5, wherein the base B is one or more of alkali metal compounds, alkaline earth metal compounds, and ammonia, preferably B is 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, and more preferably potassium hydroxide.

7. The process according to any one of claims 1 to 6, wherein no organic solvent is used in (ii).

8. (iii) However, (iii.1) F1 to Z W The process involves introducing the material into the cleaning unit UM2 provided therein, (iii.2) F1 is brought into contact with water in UM2 at a temperature T2 in the range of 10 to 95°C, and the aqueous phase P A (2) and organic phase P O A step to obtain a mixture M2 containing (2), wherein the aqueous phase P of M2 A (2) The pH is in the range of 7.5 to 11, P A (2) PH < P A (1) The pH of the process, (iii.3) The mixture M2 obtained according to (iii.2) is Z W It is provided and passes through the liquid-liquid separation unit US2 located downstream of UM2, P A Flow F including (2) A (2) and the refined pyrolysis oil P O (2) A process to obtain flow F2 including The process according to any one of claims 1 to 7, including the process described in any one of claims 1 to 7.

9. The cleaning unit UM2 is one or more of a stirring vessel, a mixing pump, and a static mixer, more preferably a stirring vessel. The process according to claim 8, wherein the liquid-liquid separation unit US2 is one or more of a hydrocyclone, a sedimentation tank, a centrifuge, and an extraction column, preferably a hydrocyclone, a sedimentation tank, or a centrifuge, more preferably a sedimentation tank or a centrifuge.

10. (iii) However, (iii.1') F1 to Z W The process involves introducing the material into the extraction column UM+US provided in the device, (iii.2') The process of introducing water into UM+US, (iii.3') F1 is brought into contact with water in UM+US at a temperature T2' ranging from 10 to 95°C, and the aqueous phase P A Flow F including (2) A (2) A step to obtain the aqueous phase P of M2 A (2) The pH is in the range of 7.5 to 11, P A (2) PH < P A (1) The process of obtaining the flow F2 containing the refined pyrolysis oil, which has a pH of (1) The process according to any one of claims 1 to 7, including the process described in any one of claims 1 to 7.

11. The process according to any one of claims 8 to 10, wherein the weight ratio of water to F1 is in the range of 0.05:1 to 2:1, preferably in the range of 0.1:1 to 1.5:1, more preferably in the range of 0.1:1 to 1.2:1, and more preferably in the range of 0.1:1 to 0.5:

1.

12. F obtained according to (iii.3) A (2) A process of recycling at least a portion of the water contained in (ii.2) and / or (iii.2), F obtained according to (iii.3') A (2) A process of recycling at least a portion of the water contained in (ii.2) and / or (iii.2') The process according to any one of claims 8 to 11, further comprising:

13. In US1, P A (1) and P O The process according to any one of claims 1 to 12, further comprising the step of purging the precipitate from US1, which is preferably a sedimentation tank, if a precipitate is formed at the interface with (1).

14. The stream F2 containing the refined pyrolysis oil obtained according to (iii) has a TAN lower than the total acid number (TAN) of the pyrolysis oil provided in (i), Preferably, the process according to any one of claims 1 to 13, wherein the flow F2 containing the refined pyrolysis oil obtained according to (iii) has an oxygen content less than or equal to, more preferably less than, the oxygen content of the pyrolysis oil provided in (i).

15. (iv) At least a portion of the flow F2 obtained according to (iii) is Z W (iv) further includes subjecting to one or more subsequent washes in (iv.1)(iii) At least a portion of F2 obtained according to (iii), preferably F2, Z W It is provided for use in the UM3 cleaning unit located downstream of US2, and can be optionally installed therein. At least a portion of F2, preferably F2, is brought into contact with water in UM3 at a temperature T3 in the range of 10 to 95°C to form an aqueous phase P A (3) and organic phase P O (3) is included, and ranges from 7.5 to 11, P A (3) PH < P A (1) A mixture M3 with the pH of (1) is obtained. Z W In the liquid-liquid separation unit US3 located downstream of UM3, the mixture M3 is passed through P A Flow F including (3) A (3) and the refined pyrolysis oil P O A process to obtain flow F3 including (3), At least a portion of F2 obtained according to (iv.2)(iii), preferably F2, or at least a portion of F3 obtained according to (iv.1), located downstream of US3, Z W The process involves introducing the material into the cleaning unit UM4 provided therein, (iv.3) At least a portion of F2 or at least a portion of F3 is brought into contact with water in UM4 at a temperature T4 in the range of 10 to 95°C to form an aqueous phase P A (4) and organic phase P O A step to obtain a mixture M4 containing (4), wherein the aqueous phase P of M4 A (4) The pH is in the range of 7.5 to 11, P A (4) PH < P A (1) The pH of the process, The mixture M4 obtained according to (iv.4)(iv.3) is Z W It is included and passed through the liquid-liquid separation unit US4 located downstream of UM4, P A Flow F including (4) A (4) and the refined pyrolysis oil P O (4) A process to obtain flow F4 including The process according to any one of claims 1 to 14, including the process described in any one of claims 1 to 14.

16. (iv) The process further includes introducing F2 containing the pyrolysis oil obtained according to (iii), and optionally F4 obtained according to (iv) of claim 15, into at least one storage unit SU to store the pyrolysis oil in SU, The process according to any one of claims 1 to 15, wherein the storage unit SU is a storage tank, preferably made of one or more of steel and stainless steel, more preferably carbon steel and stainless steel.

17. A unit for carrying out a process for refining pyrolysis oil according to any one of claims 1 to 16, - At least one extraction zone Z comprising an extraction unit UM1 and a liquid-liquid separation unit US1 E Therefore, UM1 is located upstream of US1, in extraction zone Z. E and, -F0 to Z E An entry point for introducing it, -Z E An exit means for removing F1 from, - An entry point for introducing F0 into UM1, - An exit means for removing M1 from UM1, - An entry point for introducing M1 to US1, - An exit strategy from removing F1 from US1, -Z E At least one washing zone Z located downstream W and, - F1 to Z W An entry point for introducing it, -Z W An exit means for removing F2 from and A unit equipped with [the necessary components].

18. A refined pyrolysis oil that can be obtained or is obtainable by a process described in any one of claims 1 to 16, preferably the refined pyrolysis oil of the present invention having a total acid number (TAN) in the range of 0 to 10 Mg KOH / g (oil), more preferably in the range of 0 to 4 Mg KOH / g (oil).

19. - A step of obtaining a refined pyrolysis oil, monomer, polymer, or polymer product using the unit described in claim 17. A process that includes this.

20. Preferably, - A process of converting the flow F2, which can be obtained or obtained by any one of claims 1 to 16, or a chemical substance that can be obtained or obtained by any one of claims 1 to 16, to obtain a monomer, polymer, or polymer product. A process comprising the steps of any one of claims 1 to 16, further comprising the steps of any one of claims 1 to 16.

21. The polymer or polymer product is a granular material, strand, rod, plate, pipe, foil, layer, film, sheet, fiber, filament, coating, extruded article and / or molded article, flexible foam, semi-rigid foam and / or rigid foam. The process according to claim 19 or 20.

22. The monomer is a diol or polyol; preferably butanediol; aldehyde; preferably formaldehyde; diisocyanate or polyisocyanate; preferably methylenediphenyl diisocyanate (MDI), polymeric methylenediphenyl diisocyanate (PMDI), toluene diisocyanate (TDI), hexamethylenediisocyanate (HDI), or isophorone diisocyanate (IPDI); amide; preferably caprolactam; alkene; preferably styrene, ethene, and norbornene; alkyne, (di)ester; preferably methyl methacrylate; monoacid or diacid; preferably adipic acid or terephthalic acid; diamine; preferably hexamethylenediamine, nonanediamine, or sulfone; preferably 4,4'-dichlorodiphenyl sulfone. The process according to any one of claims 19 to 21.

23. The polymer is polyamide (PA); preferably PA6 and PA66; polyisocyanate polyaddition product; preferably polyurethane (PU), thermoplastic polyurethane (TPU), polyurea or polyisocyanurate (PIR); low-density polyethylene (LDPE), high-density polyethylene (HDPE), polyethylene (PE), polypropylene (PP), polyvinyl chloride (PVC), polyvinyl acetate (PVA), polystyrene (PS), polyacrylonitrile butadiene styrene (ABS), polystyrene acrylonitrile (SAN), polyacrylate styrene acrylonitrile (ASA), polytetrafluoroethylene (TEFlON), thermoplastic polyurethane (TPU), poly(methyl acrylate) (PMA), poly(methyl methacrylate) (PMMA), polybutadiene (BR, PBD), poly(cis-1,4-isoprene), poly(TRANS-1,4-isoprene), polyoxymethylene (P OM), polyethylene terephthalate (PET), polybutylene terephthalate (PBT), polybutylene adipate copolymer (PBAT), polyester (PES), polyethersulfone (PESU), polyhydroxyalkanoate (PHA), poly-3-hydroxybutyrate (P3HB), poly-4-hydroxybutyrate (P4HB), polyhydroxyvalerate (PHV), polyhydroxyhexanoate (PHH), polyhydroxyoctanoate (PHO), polylactic acid (PLA), polysulfone (PSU), polyphenylene sulfone (PPSU), polycarbonate (PC), polyetheretherketone (PEEK), poly(P-phenylene oxide) (PPO), poly(P-phenylene ether) (PPE); and copolymers and mixtures thereof, and / or the polymer products comprising them. The process according to any one of claims 19 to 22.

24. The polymer and / or the polymer product - Parts of an automobile, preferably cylinder head covers, engine covers, housings for intake refrigerants, intake refrigerant flaps, intake pipes, intake manifolds, connectors, gear wheels, fan wheels, coolant boxes, housings or housing components for heat exchangers, coolant coolers, intake refrigerants, thermostats, water pumps, radiators, fastening components or components of battery systems for electric transport, dashboards, steering column switches, seats, headrests, center consoles, transmission components, door modules, automotive exteriors for A, B, C or D pillar covers, spoilers, door handles, exterior mirrors, windscreen wipers, windscreen wiper protective housings, decorative grilles, cover strips, roof rails, window frames, sunroof frames, antenna panels, headlights and taillights, engine covers, cylinder head covers, intake manifolds, airbags, or cushions; - Cloth, preferably shirts, trousers, pullovers, boots, shoes, soles, tights, or jackets; - Electrical components, preferably electrostatic or electroactive components or electrostatic or electroactive components, printed circuit boards, printed circuit board housing components, foil, lines, switches, plugs, sockets, distributors, relays, resistors, capacitors, inductors, bobbins, lamps, diodes, LEDs, transistors, connectors, regulators, integrated circuits (ICs), processors, controllers, memory, sensors, connectors, microswitches, microbuttons, semiconductors, reflector housings for light-emitting diodes (LEDs), fasteners, spacers, bolts, strips, slide-in guides, screws, nuts, film hinges, snap hooks (snap-ins), or spring tongues for electrical or electronic components; - Consumer products and / or pharmaceuticals, preferably tennis strings, climbing ropes, bristle, brushes, artificial grass, 3D printing filaments, grass trimmers, zippers, hook-and-loop fasteners, paper machine clothing, extruded coatings, fishing lines, fishing nets, offshore lines and ropes, vials, syringes, ampoules, bottles, sliding elements, spindle nuts, chain conveyors, plain bearings, rollers, wheels, gears, rollers, ring gears, screws and spring dampers, hoses, pipelines, cable sheathing, sockets, switches, cable ties, fan wheels, carpets, cosmetic boxes or bottles, mattresses, cushions or insulation; and / or - Packaging for the food industry; preferably single-layer or multi-layer inflation film, cast film (single-layer or multi-layer), biaxially oriented film, laminate film The process according to any one of claims 19 to 23, which is either or a part thereof.

25. The content of the pyrolysis oil in the flow F0 in the refined pyrolysis oil, monomer, polymer and / or polymer product is 1% by weight or more, preferably 2% by weight or more, more preferably 5% by weight or more, more preferably 15% by weight or more, more preferably 30% by weight or more, more preferably 40% by weight or more, more preferably 60% by weight or more, more preferably 80% by weight or more, more preferably 90% by weight or more, more preferably 95% by weight or more, and / or The content of the pyrolysis oil in the flow F0 in the refined pyrolysis oil, monomer, polymer and / or polymer product is 100% by weight or less, preferably 95% by weight or less, more preferably 90% by weight or less, more preferably 50% by weight or less, more preferably 25% by weight or less, and more preferably 10% by weight or less. Preferably, the content is determined based on an identity retention and / or separation and / or mass balance and / or book-and-claims chain of custody model, preferably based on a mass balance, preferably based on an International Sustainable Carbon Certification (ISCC) standard, according to any one of claims 19 to 24.

Images