Plastic recycling through hydrocracking

Abstract

The invention relates to a process for the production of petrochemical feedstock, comprising: (a) mechanically processing a hydrocarbon feed (A) comprising mixed waste plastic (MWP) to obtain an oligomeric product stream (OS); (b) subjecting the oligomeric product stream (OS) to a decontamination treatment to obtain a decontaminated oligomeric product stream (DOS) comprising oligomeric products; (c) combining, preferably blending, the decontaminated oligomeric product stream (DOS) with a hydrocarbon stream (HD) to obtain a hydrocarbon feed (B); (d) hydrotreating the hydrocarbon feed (B) to obtain a hydrocracking feed (HF); and (e) hydrocracking the hydrocracking feed (HF) to obtain the petrochemical feedstock; i. wherein the oligomeric product stream (OS) has a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20; and ii. wherein the hydrocracking feed (HF) has a total content of nickel and vanadium of < 150 parts per million (ppm) by weight, preferably < 100 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight; and iii. wherein the oligomeric product stream (OS) has a total olefinic content of < 5.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

Description

PLASTIC RECYCLING THROUGH HYDROCRACKING

[0001] The invention relates to a process of hydrocracking a feed derived from mixed waste plastic for producing petrochemical feedstock. The invention further relates to such a hydrocarbon feed derived from mixed waste plastic for producing petrochemical feedstock.

[0002] End of life plastics / waste plastics, pose an environmental concern when they are dumped in landfills or incinerated. Incineration of waste plastic increases greenhouse gases and also leads to air and land pollution. Alternatively, waste plastics are diverted to landfills or are incinerated, with smaller proportion being diverted to recycling. To address this, regulations are becoming more stringent and are moving towards pushing or incentivizing plastic manufacturers to incorporate more recycled material into resins supplied by them.

[0003] On the other hand there is a growing interest in making use of mixed waste plastic for producing hydrocarbon feedstock to boost circular economy operations in petrochemical industry. One possible technique for producing high value hydrocarbon products from mixed waste plastics is by hydrocracking. For example, the patent application W02023002092 describes a method of involving the use of liquefied waste plastic (LWP) and a vacuum gas oil (VGO) stream to produce a hydrocracked stream.

[0004] The process as described, relies on the use of pyrolysis to obtain the plastic waste (LWP) in a form that can be further processed. During the pyrolysis, certain amount of feed material may be lost as gas products resulting in lower carbon efficiency. In particular such a pyrolysis process converts plastic feed to a form, which is similar to crude oil having an end boiling point of 750 deg C (similar to crude oil range) and involves extensive capex for melting, pyrolysis and fractionation.

[0005] Further, another aspect to consider is that a hydrocracking operations are typically hydrogen consuming process. However, in petrochemical refineries, hydrogen is a scarce resource and utilization of hydrogen needs to be effectively managed. In recent decades environmentalpolicies and market demand have led to a significant growth in the demand for hydrogen. Typically, in an integrated refinery, the deficit of hydrogen is made up to some extent by supplying hydrogen gas obtained from auxiliary petrochemical processes such as steam reforming or partial oxidation of methane. All of such processes involve high capital and operational expenditure. Therefore, effective utilization of hydrogen is desired especially for operations involving hydrocracking of feed.

[0006] In this context, products obtained from the pyrolysis of waste plastics, are typically richer in olefins and other unsaturated products compared to other conventional feed. Pyrolysis process results in liquid pyrolysis products containing ~30-40wt% olefins, including diolefins, and generation of additional aromatics (-3-10 wt.%). This high degree of unsaturation consumes additional hydrogen during a hydrocracking process compared to a feed having lower olefin content. Moreover, during pyrolysis there may be as high as 15.0 wt.% loss of hydrogen-rich gases, which effectively means the loss of hydrogen from the plastic feed and results in liquid products that have high content of unsaturated compounds. Therefore, feed obtained from pyrolysis such as pyrolysis oil when used in hydrocracker units may result in the consumption of additional hydrogen, which negatively affects the overall hydrogen management of the process.

[0007] Further, diolefins that are formed during the pyrolysis, may convert to gum during transportation and storage resulting in the loss of feed material.

[0008] Therefore, it is an object of the present invention, to provide a process for the conversion of mixed waste plastics into petrochemical feedstock while ensuring efficient use of hydrogen and retaining carbon efficiency during the course of hydrocracking. It is yet another objective of the invention to obtain a hydrocracking feed suitable for producing petrochemical feed stock, that has a suitable composition to be hydrocracked with the efficient use of hydrogen and retaining carbon efficiency.

[0009] Such is now achieved by a process for the production of petrochemical feedstock, comprising:(a) mechanically processing a hydrocarbon feed (A) comprising mixed waste plastic (MWP) to obtain an oligomeric product stream (OS);(b) subjecting the oligomeric product stream (OS) to a decontamination treatment to obtain a decontaminated oligomeric product stream (DOS) comprising oligomeric products;(c) combining, preferably blending, the decontaminated oligomeric product stream (DOS) with a hydrocarbon stream (HD) to obtain a hydrocarbon feed (B);(d) hydrotreating the hydrocarbon feed (B) to obtain a hydrocracking feed (HF); and(e) hydrocracking the hydrocracking feed (HF) to obtain the petrochemical feedstock.

[0010] The oligomeric product stream (OS) has a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20.

[0011] The hydrocracking feed (HF) has a total content of nickel and vanadium of < 150 parts per million (ppm) by weight, preferably < 100 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight, with regard to the total weight of the hydrocracking feed (HF). The oligomeric product stream (OS) has a total olefinic content of < 5.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

[0012] The oligomeric product stream (OS), may be a partially depolymerized material produced from the hydrocarbon feed A and has molecular weight higher than petroleum crude oil molecular weight i.e. higher molecular weight greater than C120H242 (mol.wt 1682 g / mol).

[0013] In certain instances, the boiling point of the oligomeric product stream (OS) may not be specifically determined as the oligomeric product stream (OS) at high temperature starts cracking. It is preferred that the decontaminated oligomeric product stream (DOS) and theoligomeric product stream (DOS) have similar, preferable identical, weight average molecular weight, olefinic and aromatic content.

[0014] Advantageously, the process of the present invention allows for the efficient use of hydrogen for the conversion of mixed plastic waste to petrochemical feedstock. For example, in the context of the process of the present invention, for an identical ratio of flow rate of hydrogen to the flow rate of hydrocracking feed (HF) and for an identical feed conversion, the hydrocracking feed (HF) is hydrocracked with lesser hydrogen consumption as compared to the hydrocracking of a similar hydrocracking feed which is not derived from the decontaminated oligomeric product stream (DOS).

[0015] The term “feed conversion” as used herein means the conversion of the hydrocracking feed (HF) to a petrochemical feedstock. The term “not derived from the decontaminated oligomeric product stream (DOS)” as used in this disclosure means a hydrocarbon feedstream which has not been obtained by upstream processing or treatment of the decontaminated oligomeric product stream (DOS).

[0016] As an associated benefit in terms of efficient use of hydrogen, for an identical proportion of H2 / Hydrocarbon feed (HF) expressed in Nm3 / m3and for an identical amount of hydrogen consumption, a higher quantity of hydrocracking feed (HF) comprising the decontaminated oligomeric product stream (DOS) may be hydrocracked as compared to a hydrocracking feed, which is free of the decontaminated oligomeric product stream (DOS). The quantity of products formed from hydrocracking may be expressed in tons / hr.

[0017] Advantageously, in comparison to the pyrolysis of waste plastics, the mechanical processing of the waste plastic to oligomeric product stream has a higher carbon conversion due to lower loss of feed material through the formation of gaseous byproducts.Mechanical processing:

[0018] The hydrocarbon feed (A) is mechanically processed to obtain the oligomeric product stream (OS). The term “mechanical processing” as used herein means a thermo-mechanical process or a process, which involves the generation of heat from the mechanical shearing of the hydrocarbon feed or through the external supply of heat. It is particularly preferred that the generated heat through mechanical processing is sufficient to melt the hydrocarbon feed and / or crack the hydrocarbon feed (A).

[0019] The mechanical processing of the hydrocarbon feed (A) comprises at least one step selected from melt extrusion, compacting, mechanical agitation, and any combinations thereof. Preferably, the mechanical processing of the hydrocarbon feed (A) comprises the step of melt extruding the hydrocarbon feed (A).

[0020] During the step of melt processing, the hydrocarbon feed (A) is melt cracked to form the oligomeric product stream (OS). It is particularly preferred that the mechanical processing of the hydrocarbon feed (A) is carried out in the absence of hydrogen gas and / or a catalyst.

[0021] Preferably, the step of melt extruding the hydrocarbon feed (A) comprises the steps of supplying the hydrocarbon feed (A) in a de-volatilization extruder; and melt extruding the hydrocarbon feed (A) under conditions of (a) temperature of > 250 °C and < 450 °C, preferably > 300 °C and < 450 °C; and (b) at a feed residence time of > 0.1 minute and < 60.0 minutes. Preferably, the hydrocarbon feed (A) is extruded at a temperature of > 300 °C and < 400 °C, preferably > 350 °C and < 410 °C. Preferably, the hydrocarbon feed (A) is extruded at a feed residence time of > 0.1 minute and < 60.0 minutes, preferably > 1.0 minute and < 40.0 minutes, preferably > 5.0 minute and < 30.0 minutes, preferably > 5.0 minute and < 10.0 minutes. The term “residence time” as used throughout the disclosure means the total time the hydrocarbon feed (A) is mechanically processed or melt extruded.

[0022] The de-volatilization extruder may comprise a first section where the hydrocarbon feed (A) is introduced and subsequently melt extruded and dechlorinated at temperatures of < 350 °C, preferably > 260 °C and < 300 °C. The de-volatilization extruder may further comprise a second section wherein the melt extruded hydrocarbon feed (A) from the first section is heated, de-chlorinated and cracked to a form the oligomeric product stream (OS) under conditions oftemperature of > 300 °C and < 450 °C. The first section of the extruder comprises > 20% and < 90% of total length of extruder, preferably < 70%, preferably < 50% of the total length of extruder.

[0023] Preferably, the melt extrusion is carried out at a pressure of > 1 atm absolute (atma) and > 10'14Torr, preferably > 0.1 atma and < latm gauge (atmg). Alternatively, the melt extrusion may be operated under vacuum conditions, i.e., at pressures below ambient pressure (e.g., below 1 atm).

[0024] It is preferred that the feed residence time is kept lower than the residence time used typically in a pyrolysis while maintaining the temperature of mechanical processing < 450 °C. Such a process configuration helps in limiting the amount of olefins and aromatics formed during the mechanical processing. Advantageously, such a process configuration mitigates the loss of hydrocarbon gases during mechanical processing to < 5.0 wt%, preferably < 3.0 wt%, with regard to the total weight of the hydrocarbon feed (A).

[0025] With a suitable control of residence time and temperature, the overall content of unsaturated compounds such as olefins and aromatics is kept at a level suitable for hydrocracking resulting in efficient hydrogen utilization. It is preferred that the oligomeric product stream (OS) comprises: (a) a total olefinic content of < 5.0 wt.%, preferably < 2.0 wt.%, preferably < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS); and / or (b) a total aromatic content of < 10.0 wt.%, preferably < 5.0 wt.%, preferably < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

[0026] Preferably the oligomeric product stream (OS) comprises: a total olefinic content of > 0.0 wt.% and < 5.0 wt.%, preferably > 0.0 wt.% and < 2.0 wt.%, preferably > 0.0 wt.% and < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS). It is particularly, preferred that the olefinic products in the oligomeric product stream (OS) comprises olefins having a weight average molecular weight of > 1682 g / mole when determined in accordance with ASTM D6474-20.

[0027] Preferably, the oligomeric product stream (OS) comprises a total aromatic content of > 0.0 and < 10.0 wt.%, preferably > 0.0 and < 5.0 wt.%, preferably > 0.0 and < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS). It is particularly preferred that the aromatic products in the oligomeric product stream (OS) comprise aromatic compounds having a weight average molecular weight of > 1682 g / mole when determined in accordance with ASTM D6474-20.

[0028] Preferably, wherein the amount of aromatic compounds formed during the mechanical processing of the hydrocarbon feed (A) is < 10.0 wt.%, preferably < 5.0 wt.%, preferably < 1.0 wt.% of the total aromatic compounds present in the hydrocarbon feed (A).

[0029] The content of olefinic and aromatic content may be determined by using NMR or FT-IR spectroscopic analysis or by supercritical fluid chromatography. Preferably, the olefinic content is measured using supercritical fluid chromatography in accordance with ASTM-D6550- 05. Preferably, the olefinic and aromatic content may be determined using FT-IR spectroscopic analysis in accordance with ASTM D5576-00 (2006). The molecular weight can be determined by gel permeation chromatography (GPC) technique in accordance with ASTM D6474-20.

[0030] It is preferred that the hydrocarbon feed (A) comprises > 80.0 wt.%, preferably > 90.0 wt.%, preferably > 95.0 wt.%, preferably 100.0 wt.%, of mixed waste plastic (MWP) with regard to the total weight of the hydrocarbon feed (A).

[0031] Preferably, wherein the mixed waste plastic (MWP) comprises at least one polymer selected from polypropylene, polyethylene, polyester, polystyrene, natural and / or synthetic rubber, polyolefin elastomers, polycarbonate, polyvinyl chloride and mixtures thereof. Non-limiting examples of polyethylene include high density polyethylene, linear low density polyethylene, low density polyethylene, and ethylene copolymers. Non limiting examples of polypropylene can be polypropylene homopolymers or polypropylene copolymers, heterophasic polypropylene. Non limiting examples of polycarbonate include polycarbonate homopolymers and co-polymers and blends of polycarbonate with thermoplastics as polyesters.

[0032] Preferably, the mixed waste plastic include mixtures comprising polyolefins, polyesters, thermoplastic elastomers, polyvinyl chlorides, polystyrenes, or polycarbonates. In particular, the mixed waste plastic can be mixtures comprising > 25.0 wt% of polyolefins, with regard to the total weight of the mixed waste plastic. Preferably, the mixed waste plastic may comprise > 40.0 wt%, preferably > 50.0 wt%, preferably > 60.0 wt%, preferably > 70.0 wt%, preferably >80.0 wt.%, preferably > 90.0 wt.%, preferably > 98.0 wt.%, of polyolefins, with regard to the total weight of the mixed waste plastic.

[0033] The mixed waste plastic may comprise a fraction of non-thermoplastic materials. Such non-thermoplastic materials may include hydrocarbon-based materials, such as rubber materials, but may also be materials including paper, sand and soil. It is an advantage of the present invention that mixed waste plastic may contain < 10.0 wt%, preferably < 5.0 wt%, more preferably < 2.0 wt%, of materials selected from paper, sand and soil, and combinations thereof.

[0034] The mechanical processing of the hydrocarbon feed (A) results in the formation of oligomers having reduced molecular weight compared to the polymers constituting mixed waste plastic (MWP). For example, the oligomeric product stream (OS) has a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20.

[0035] The melt extrusion and cracking of the hydrocarbon (A) may be carried out in a single screw extruders, twin-screw extruders, twin-screw co-rotating extruders, banbury mixers, BUSS mixing extruders. During the process, chlorine containing resins (e.g. PVC) may generate hydrochloric acid which may be subsequently removed through an extruder vent in presence of / absence of N2 stripping gas or by partial vacuum application.Decontamination treatment:

[0036] The oligomeric product stream (OS) once obtained, is subjected to a decontamination treatment to obtain a decontaminated oligomeric product stream (DOS)comprising oligomeric products. The decontamination treatment is carried out to remove impurities such as silicon, phosphorous, chlorides, iron and / or other metallic / non-metallic heteroatoms from the oligomeric product stream (OS).

[0037] The decontaminated oligomeric product stream (DOS) comprising oligomeric products may have a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20.

[0038] Preferably, the decontamination treatment comprises at least one process step selected from (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant hydrocarbon stream through a melt filter to obtain the decontaminated oligomeric product stream (DOS), (ii) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant stream, through a melt filter and subsequently through an adsorbent guard bed, preferably in the presence of hydrogen, to obtain the decontaminated oligomeric product stream (DOS), (iii) mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 350 °C followed by an alkaline treatment at a temperature of > 200 °C and < 350 °C prior to obtaining the decontaminated oligomeric product stream (DOS), (v) mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 430 °C, and passing the resultant stream, through a melt filter and subsequently over a demetallization catalyst in presence of hydrogen to obtain the decontaminated oligomeric product stream (DOS), (vi) passing the oligomeric product stream (OS) over a de-metallization catalyst in presence of hydrogen, to obtain the decontaminated oligomeric product stream (DOS), and (vii) any combinations thereof.

[0039] It is particularly preferred that the decontamination treatment comprises the step of mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 430 °C, and passing the resultant stream, through a melt filter and subsequently over a demetallization catalyst, in presence of hydrogen, to obtain the decontaminated oligomeric product stream (DOS).

[0040] It is particularly preferred that the decontamination treatment comprises the step of mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 350 °C followed an by alkaline treatment at temperature of > 200 °C and < 350 °C, prior to obtaining the decontaminated oligomeric product stream (DOS).

[0041] The alkaline treatment may comprise the step of adding in an amount of > 0.1 and < 10.0 mol / L of an aqueous alkali metal hydroxide solution to the hydrocarbon solvent containing oligomeric product stream (OS). The alkali metal hydroxide may be any one of sodium hydroxide or potassium hydroxide. Preferably, the alkali metal hydroxide is sodium hydroxide. The addition of an aqueous alkali metal hydroxide solution results in the formation of an aqueous alkali phase stream and a hydrocarbon phase stream. The aqueous alkali phase stream may be separated from the hydrocarbon phase stream to obtain the decontaminated oligomeric product stream (DOS).

[0042] Preferably, the ratio of the aqueous solution of alkaline metal hydroxide to the hydrocarbon solvent containing the oligomeric product stream (OS) is > 0.1 g / g, preferably from > 0.5 and < 1.5 g / g.

[0043] Preferably, wherein the decontamination treatment comprises the steps of (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 350 °C to obtain a stream (P) (ii) adding an aqueous alkali metal hydroxide solution to stream (P) at temperature of > 200 °C and < 350 °C to obtain an alkaline phase stream and a hydrocarbon phase stream, and (iii) separating the alkaline phase stream from the hydrocarbon phase stream to obtain the decontaminated oligomeric product stream (DOS).

[0044] During alkaline treatment, a temperature of > 200 °C and < 350 °C may be maintained for a time duration of > 1.0 and < 180.0 min, preferably from > 2.0 and < 90.0 min, more preferably from > 5.0 and < 60.0 min.

[0045] Preferably, the hydrocarbon solvent is any one of heavy gas oil (HGO), light cycle oil (LCO), vacuum gas oil (VGO), atmospheric residue (AR), vacuum residue (VR), whole crudeoil, cuts of crude oil, and mixtures thereof. Preferably, the hydrocarbon solvent is vacuum gas oil (VGO).

[0046] The term "vacuum gas oil stream" or "VGO" stream as used here means a stream of heavy oils, which are recovered as distillates from an oil refinery vacuum distillation unit. The VGO / HGO stream contains a large quantity of cyclic and aromatic compounds as well as heteroatoms, such as sulphur and nitrogen, and other heavier compounds. The exact composition of the VGO / HGO stream varies depending on the crude source used for petroleum distillation and the VGO / HGO cut-off.

[0047] Preferably, the decontamination treatment of the oligomeric product stream (OS) comprises the step of (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant hydrocarbon stream through a melt filter to obtain a filtrate stream (F); (ii) passing the filtrate stream (F), preferably in the presence of hydrogen, through an adsorbent guard bed at a temperature of > 200 °C and < 350 °C to obtain the decontaminated oligomeric product stream (DOS) after separating the hydrocarbon solvent.

[0048] The adsorbent guard bed is typically selected from silica-based adsorbents or large pore alumina. Preferably the adsorbent is trisyl silica. The oligomeric product stream is passed through this bed of adsorbent at 0.1-lOHr1WHSV when a fixed bed guard bed is employed. When a slurry / stirred tank / tubular flow reactor is used, the amount of adsorbent used is typically from > 0.1 and < 10.0 wt%, preferably > 0.5 and < 2.0 wt.%, of the total weight of the oligomeric product stream (OS).Hydrocarbon feed (B)

[0049] The decontaminated oligomeric product stream (DOS) may be combined, preferably blended, with a hydrocarbon stream (HD) to obtain a hydrocarbon feed (B).

[0050] Preferably, wherein the hydrocarbon feed (B) comprises: (a) > 0.1 wt.% and < 90.0 wt.% of the decontaminated oligomeric product stream (DOS); and (b) > 10.0 wt.% and < 99.9 wt.% of the hydrocarbon stream (HD); with regard to the total weight of the hydrocarbon feed (B).

[0051] Preferably, wherein the hydrocarbon feed (B) comprises: (a) > 1.0 wt.% and < 90.0 wt.% of the decontaminated oligomeric product stream (DOS); and (b) > 10.0 wt.% and < 99.0 wt.% of the hydrocarbon stream (HD); with regard to the total weight of the hydrocarbon feed (B).

[0052] Preferably, wherein the hydrocarbon feed (B) comprises: (a) > 5.0 wt.% and < 10.0 wt.% of the decontaminated oligomeric product stream (DOS); and (b) > 90.0 wt.% and < 95.0 wt.% of the hydrocarbon stream (HD); with regard to the total weight of the hydrocarbon feed (B).

[0053] Preferably, wherein the hydrocarbon stream (HD) and the hydrocarbon solvent used for the decontamination treatment are identical having identical chemical and physical properties.

[0054] Preferably wherein the hydrocarbon stream (HD) is selected from heavy gas oil (HGO), light cycle oil (LCO), vacuum gas oil (VGO), atmospheric residue (AR), vacuum residue (VR), whole crude oil, cuts of crude oil, condensates, and mixtures thereof. Preferably wherein the hydrocarbon stream (HD) is vacuum gas oil (VGO).

[0055] Preferably, wherein the hydrocarbon feed (B) comprises: (a) > 0.1 and < 90.0 wt.% of the decontaminated oligomeric product stream (DOS); and (b) > 10.0 wt.% and < 99.9 wt.% of vacuum gas oil (VGO); with regard to the total weight of the hydrocarbon feed (B).

[0056] Preferably, wherein the hydrocarbon feed (B) comprises: (a) > 5.0 and < 10.0 wt.% of the decontaminated oligomeric product stream (DOS); and (b) > 90.0 wt.% and < 95.0 wt.% of vacuum gas oil (VGO); with regard to the total weight of the hydrocarbon feed (B).Hydro-treatment of Hydrocarbon feed (B)

[0057] The hydrocarbon feed (B) is hydrotreated to obtain a hydrocracking feed (HF). The hydrotreatment process may be performed under conditions suitable to remove heteroatoms such as oxygen, sulphur and / or nitrogen from the hydrocarbon feed (B). In addition, the hydrotreatmentof the hydrocarbon feed (B) may result in full or partial saturation of any residual unsaturated compounds (aromatics and olefins) that may be present in the feed.

[0058] The hydrotreatment process may be carried out in the presence of a supported catalyst. Examples of such supported catalyst include supported NiMo catalyst or a supported CoMo catalyst, CoNiMO, tungsten molybdenum catalyst, nickel catalyst or a mixture thereof. Preferably, the catalyst support comprises any one of alumina and / or silica.

[0059] The hydrotreatment process may be carried out under any suitable hydrotreating conditions. For example, the hydrotreating of the hydrocarbon feed (B) is performed at a temperature of > 180 °C and < 450 °C, preferably > 280 °C and < 430 °C, preferably > 300 °C and < 430 °C while the pressure may be maintained at > 3.0 MPa and < 25.0 MPa, preferably > 7.0 MPa and < 18.0 MPa, preferably from > 10.0 MPa and < 17.5 MPa. The hydrogen to feed ratio during hydro-treating may be maintained at 200-3000 NL H2 / L hydrotreating feed, preferably 600- 1300 NL H2 / L hydrotreating feed and more preferably 800-1000 NL H2 / L hydrotreating feed; and a hydrocarbon liquid hourly space velocity (LHSV) of > 0.2 and < 10.0 1 / h, preferably > 0.9 and < 2.7 1 / h and more preferably > 1.0 and < 2.5 1 / h.Hydrocracking Feed (HF)

[0060] The term hydrocracking feed (HF) as used in this disclosure means a hydrocarbon feed that is hydrocracked to obtain the petrochemical feedstock. The hydrocracking feed once obtained may be further treated to remove any residual sulfur, nitrogen, chlorides, metal and other hetero atoms.

[0061] Preferably, wherein the hydrocracking feed (HF) is subjected to hydrodemetallization and / or hydro-desulfurization treatment prior to hydrocracking. Preferably wherein the hydrodemetallization and / or hydrodesulfurization treatment is carried out at a temperature of > 280 °C and < 430 °C, preferably > 300 °C and < 400 °C and at a partial pressure of > 4.0 MPa and < 20.0 MPa, preferably > 4.0 MPa and < 8.0 MPa.

[0062] The hydrocracking feed (HF) has a sufficiently low amount nickel, vanadium, elemental sulfur, silicon, atomic nitrogen, for the purpose of hydrocracking the feed without adversely affecting the performance of the hydrocracking catalyst. Accordingly, the hydrocracking feed (HF) has a total content of nickel and vanadium of < 150 parts per million (ppm) by weight, preferably < 100 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight.

[0063] Preferably wherein the hydrocracking feed (HF) has an amount of nickel (Ni) of < 3.0 parts per million (ppm) by weight and an amount of vanadium (V) of < 2.0 parts per million (ppm) by weight.

[0064] Preferably wherein the hydrocracking feed (HF) has: (a) has an amount of nickel (Ni) of < 3.0 parts per million (ppm) by weight and an amount of vanadium (V) of < 2.0 parts per million (ppm) by weight; and / or (b) a total content of atomic sulfur of < 5.0 wt.%, preferably < 2.0 wt.%, with regard to the total weight of the hydrocracking feed (HF) as determined in accordance with ASTM D5453 (2012); and / or (c) a total content of atomic nitrogen of <3000 parts per million (ppm) by weight, preferably <500 parts per million (ppm) by weight, as determined in accordance with ASTM D5762 (2012); and / or (d) a silicon content of < 2.0 parts per million (ppm) by weight determined in accordance with ASTM D6130.

[0065] Preferably wherein the hydrocracking feed (HF) has: (a) has an amount of nickel (Ni) of < 3.0 parts per million (ppm) by weight and an amount of vanadium (V) of < 2.0 parts per million (ppm) by weight; and (b) a total content of atomic sulfur of < 5.0 wt.%, preferably < 2.0 wt.%, with regard to the total weight of the hydrocracking feed (HF) as determined in accordance with ASTM D5453 (2012); and (c) a total content of atomic nitrogen of <3000 parts per million (ppm) by weight, preferably <500 parts per million (ppm) by weight, as determined in accordance with ASTM D5762 (2012); and (d) a silicon content of < 2.0 parts per million (ppm) by weight determined in accordance with ASTM D6130.

[0066] Preferably wherein the hydrocracking feed (HF) has a total content of nickel and vanadium of > 0 and < 150.0 parts per million (ppm) by weight, preferably > 0 and < 100.0 parts per million (ppm) by weight, preferably > 0.5 and < 50.0 parts per million (ppm) by weight, preferably > 0.5 and < 15.0 parts per million (ppm) by weight, preferably > 0.5 and < 5.0 parts per million (ppm) by weight.

[0067] Preferably, wherein the hydrocracking feed (HF) has a total content of atomic sulfur of > 0 and < 5.0 wt.%, preferably > 0 and < 2.0 wt.%, with regard to the total weight of the hydrocracking feed (HF) as determined in accordance with ASTM D5453 (2012).

[0068] Preferably wherein the hydrocracking feed (HF) has a total content of atomic nitrogen of > 0 and < 3000 parts per million (ppm) by weight, preferably > 10.0 and < 500 parts per million (ppm) by weight, preferably > 10.0 and < 500 parts per million (ppm) by weight as determined in accordance with ASTM D5762 (2012).

[0069] Preferably wherein the hydrocracking feed (HF) has a silicon content of > 0 and < 2.0 parts per million (ppm) by weight determined in accordance with ASTM D6130.

[0070] In an aspect of the invention, the invention relates to a hydrocracking feed (HF) obtained according to the process of this invention. Preferably, wherein the hydrocracking feed (HF) has each of:(a) a total content of nickel and vanadium of < 150.0 parts per million (ppm) by weight, preferably < 100.0 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight; and(b) a total content of atomic sulfur of < 5.0 wt.%, preferably < 2.0 wt.%, with regard to the total weight of the hydrocracking feed (HF) as determined in accordance with ASTM D5453 (2012); and(c) a total content of atomic nitrogen of <3000 parts per million (ppm) by weight, preferably <500 parts per million (ppm) by weight, as determined in accordance with ASTM D5762 (2012); and(d) a silicon content of < 2.0 parts per million (ppm) by weight determined in accordance with ASTM D6130; and(e) a total olefinic content of < 5.0 wt.%, with regard to the total weight of the hydrocracking feed (HF).Hydrocracking the Hydrocracking feed (HF)

[0071] The hydrocracking feed (HF) once obtained with the desired compositional specification is subjected to hydrocracking to obtain the petrochemical feedstock.

[0072] The term “petrochemical feedstock” as used in this disclosure means gas and liquid feedstocks, which may be used for further petrochemical processing. Non-limiting examples of such petrochemical feedstock include: mixtures containing at least two or more components selected from Ci-C4( boiling at <35 °C) hydrocarbons, naphthas, Cs- C 12 hydrocarbons having boiling point in the range of (35-220 °C), C13-C22 hydrocarbons having boiling point in the range of (220-370 °C) (full range diesel), C22+ hydrocarbons having boiling point in the range of (> 370 °C), and combination thereof.

[0073] In the hydrocracking step, heteroatoms such as N and S, which have not been previously removed in the hydrotreatment process, may be removed. In the hydrocracking step mainly long-chain hydrocarbons are cleaved into short-chain hydrocarbons and / or some cyclic hydrocarbons which may undergo ring-opening reaction to form linear and / or branched hydrocarbons.

[0074] Hydrocracking process may be typically performed in the presence of a hydrocracking catalyst. Hydrocracking catalysts suitable for use in this step include but are not limited to bifunctional catalysts comprising an acidic support such as alumina, amorphous silica- alumina or a zeolite and at least one active hydrogenation component selected from IUPAC group 6, 8 or 10 of the Periodic Table of Elements. Examples of typical hydrocracking catalysts include e.g. NiW / AI2O3, NiW / zeolite, NiW / AhCh-SiCh, Pt / zeolite or Pd / zeolite, and Pt / AhCh-SiCh or Pt / AhCh-SiCh.

[0075] The hydrocracking catalyst(s) may be arranged in one or more layers in a fixed bed reactor. The hydrocracking feed (HF) together with hydrogen is directed through the fixed bed with layered hydrocracking catalyst(s) to obtain the petrochemical feedstock.

[0076] The hydrocracking feed (HF) may be hydrocracked under the following conditions: at a temperature of > 280 °C and < 450 °C, preferably > 300 °C and <430 °C and more preferably > 330 and < 430 °C; at a pressure of > 5.0 and < 25.0 MPa, preferably > 14.0 and < 18.0 MPa and more preferably > 14.5 and < 17.5 MPa; a hydrogen to feed ratio of 500 - 3000NL of H2 / L of hydrocracking feed (HF), preferably about 900 - 1300NL of H2 / L of hydrocracking feed (HF) and more preferably 1000 - 1200 NL of H2 / L of hydrocracking feed (HF); and a hydrocarbon liquid hourly space velocity (LHSV) of > 0.5 and < 5.0 1 / h, preferably > 1.0 and < 2.5 1 / h and more preferably > 1.4 and < 1.9 1 / h.

[0077] The inventors surprisingly found that the hydrocracking of the hydrocracking feed (HF) was able to be carried out at a suitable hydrogen partial pressure. Preferably wherein for an identical hydrogen feed rate in the hydrocracking reactor as expressed in terms of Gas Hourly Speed Velocity (GHSV) or H2 / Hydrocarbon liquid expressed in Nm3 / m3, the hydrocracking feed (HF) derived from the decontaminated oligomeric product stream (DOS) is hydrocracked in presence of a higher hydrogen partial pressure at the same hydrocracker total pressure as compared to a similar hydrocracking feed, which is not derived from the decontaminated oligomeric product stream (DOS).

[0078] The inventors surprisingly found that by using the process of the present invention, improved hydrogen efficiency is achieved during the process of hydrocracking a feed derived from mixed waste plastic (MWP).

[0079] In an aspect of the invention, the invention relates to a process for the production of petrochemical feedstock, the process comprises:(a) melt extruding the hydrocarbon feed (A) comprising mixed waste plastic (MWP) to obtain the oligomeric product stream (OS);(b) subjecting the oligomeric product stream (OS) to the decontamination treatment to obtain the decontaminated oligomeric product stream (DOS) comprising oligomeric products;(c) combining, preferably blending, the decontaminated oligomeric product stream (DOS) with a vacuum gas oil to obtain a hydrocarbon feed (B);(d) hydrotreating the hydrocarbon feed (B) to obtain a hydrocracking feed (HF); and(e) hydrocracking the hydrocracking feed (HF) to obtain the petrochemical feedstock;(i) wherein the oligomeric product stream (OS) has a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20; and(ii) wherein the hydrocracking feed (HF) has a total content of nickel and vanadium of < 150 parts per million (ppm) by weight, preferably < 100 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight; and(iii) wherein the decontamination treatment comprises the steps of (i) mixing the oligomeric product stream (OS) in vacuum gas oil (VGO) at a temperature of > 200 °C and < 350 °C to obtain a stream (P), (ii) adding an aqueous sodium hydroxide solution to stream (P) at temperature of > 200 °C and < 350 °C to obtain the alkaline phase stream and the hydrocarbon phase stream, and (iii) separating the alkaline phase stream from the hydrocarbon phase stream to obtain the decontaminated oligomeric product stream (DOS); and(iv) the oligomeric product stream (OS) comprises: a total olefinic content of > 0.0 wt.% and < 5.0 wt.%, preferably > 0.0 wt.% and < 2.0 wt.%, preferably > 0.0 wt.% and < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

[0080] In an another aspect, the invention relates to a process for the production of petrochemical feedstock, the process comprises:(a) melt extruding the hydrocarbon feed (A) comprising mixed waste plastic (MWP) to obtain the oligomeric product stream (OS);(b) subjecting the oligomeric product stream (OS) to the decontamination treatment to obtain the decontaminated oligomeric product stream (DOS) comprising oligomeric products;(c) combining, preferably blending, the decontaminated oligomeric product stream (DOS) with a vacuum gas oil to obtain a hydrocarbon feed (B);(d) hydrotreating the hydrocarbon feed (B) to obtain a hydrocracking feed (HF); and(e) hydrocracking the hydrocracking feed (HF) to obtain the petrochemical feedstock;(i) wherein the oligomeric product stream (OS) has a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20; and(ii) wherein the hydrocracking feed (HF) has a total content of nickel and vanadium of < 150 parts per million (ppm) by weight, preferably < 100 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight; and(iii) wherein the decontamination treatment of the oligomeric product stream (OS) comprises the step of (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant hydrocarbon stream through a melt filter to obtain a filtrate stream (F); (ii) passing the filtrate stream (F), preferably in the presence of hydrogen, through an adsorbent guard bed at a temperature of > 200 °C and < 350 °C to obtain the decontaminated oligomeric product stream (DOS) after separating the hydrocarbon solvent; and(iv) the oligomeric product stream (OS) comprises: a total olefinic content of > 0.0 wt.% and < 5.0 wt.%, preferably > 0.0 wt.% and < 2.0 wt.%, preferably > 0.0 wt.% and < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

[0081] The petrochemical feedstock may be subjected to a fractionation step two obtain one or more fractions of hydrocarbons. The fractionation of the petrochemical feedstock may be performed by typical distillation methods and one or several fractions may be obtained in the distillation. Preferably, the petrochemical feedstock may be subjected to a step of fractionation to obtain at least two fractions comprising a light fraction and a heavy fraction.

[0082] The heavy fraction may comprise hydrocarbons suitable for the production of base oil components and the light fraction comprises hydrocarbons suitable for use as fuel components or as feeds for steam cracking and subsequent polymer production.

[0083] Preferably, the fractionation of the petrochemical feedstock may be performed such as to obtain at least three fractions of which a first and a second fraction are heavier fractions comprising hydrocarbons suitable for producing base oil components and a third fraction is a lighter fraction suitable for use as fuel components or as feeds for steam cracking and subsequent polymer production. The first heavier fraction may be a fraction with components having a 5 wt.% distillation point of > 380 °C and the second heavier fraction may be a fraction with component having a 5.0 to 95.0 wt.% distillation range from > 330 °C and < 410 °C and the third fraction suitable for use as fuel components or as feeds for steam cracking and sub sequent polymer production having a boiling point distribution that is lighter than the aforementioned first and second heavier fractions and has a 95.0 wt.% distillation point of < 370 °C.

Claims

CLAIMS1. A process for the production of petrochemical feedstock, comprising:(a) mechanically processing a hydrocarbon feed (A) comprising mixed waste plastic (MWP) to obtain an oligomeric product stream (OS);(b) subjecting the oligomeric product stream (OS) to a decontamination treatment to obtain a decontaminated oligomeric product stream (DOS) comprising oligomeric products;(c) combining, preferably blending, the decontaminated oligomeric product stream (DOS) with a hydrocarbon stream (HD) to obtain a hydrocarbon feed (B);(d) hydrotreating the hydrocarbon feed (B) to obtain a hydrocracking feed (HF); and(e) hydrocracking the hydrocracking feed (HF) to obtain the petrochemical feedstock; i. wherein the oligomeric product stream (OS) has a weight average molecular weight of > 1682 and < 100,000 g / mol, preferably > 1682 and < 50,000 g / mol, preferably > 1682 and < 20,000 g / mol, preferably > 1682 and < 10,000 g / mol, preferably > 1682 and < 8,000 g / mol, preferably > 1682 and < 5,000 g / mol, preferably > 1682 and < 2,000 g / mol, when determined in accordance with ASTM D6474-20; and ii. wherein the hydrocracking feed (HF) has a total content of nickel and vanadium of< 150 parts per million (ppm) by weight, preferably < 100 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight with regard to the total weight of the hydrocracking feed (HF); and iii. wherein the oligomeric product stream (OS) has a total olefinic content of < 5.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

2. The process of claim 1, wherein the oligomeric product stream (OS) comprises:(a) a total olefinic content of < 2.0 wt.%, preferably < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS); and / or(b) a total aromatic content of < 10.0 wt.%, preferably < 5.0 wt.%, preferably < 1.0 wt.%, with regard to the total weight of the oligomeric product stream (OS).

3. The process according to any one of claims 1-2, wherein the hydrocracking feed (HF) is subjected to hydrodemetallization and / or hydrodesulfurization treatment prior to hydrocracking, preferably wherein the hydrodemetallization and / or hydrodesulfurization treatment is carried out at a temperature of > 280 °C and < 430 °C, preferably > 300 °C and < 400 °C and at a partial pressure of > 4.0 MPa and < 20.0 MPa, preferably > 4.0 MPa and < 8.0 MPa.

4. The process according to any one of claims 1-3, wherein the hydrocracking feed (HF) has(a) (a) an amount of nickel (Ni) of < 3.0 parts per million (ppm) by weight and an amount of vanadium (V) of < 2.0 parts per million (ppm) by weight; and / or(b) a total content of atomic sulfur of < 5.0 wt.%, preferably < 2.0 wt.%, with regard to the total weight of the hydrocracking feed (HF) as determined in accordance with ASTM D5453 (2012); and / or(c) a total content of atomic nitrogen of <3000 parts per million (ppm) by weight, preferably <500 parts per million (ppm) by weight, as determined in accordance with ASTM D5762 (2012); and / or(d) a silicon content of < 2.0 parts per million (ppm) by weight determined in accordance with ASTM D6130.

5. The process according to any one of claims 1-4, wherein the amount of aromatic compounds formed during the mechanical processing of the hydrocarbon feed (A) is < 10.0 wt.%, preferably < 5.0 wt.%, preferably < 1.0 wt.% of the total aromatic compounds present in the hydrocarbon feed (A).

6. The process according to any one of claims 1-5, wherein the hydrocarbon feed (A) comprises > 80.0 wt.%, preferably > 90.0 wt.%, preferably > 95.0 wt.%, preferably 100 wt.% of mixed waste plastic (MWP) with regard to the total weight of the hydrocarbon feed (A).

7. The process according to any one of claims 1-6, wherein the mixed waste plastic (MWP) comprises at least one polymer selected from polypropylene, polyethylene, polyester, polystyrene, natural and / or synthetic rubber, polyolefin elastomers, polycarbonate, polyvinyl chloride and mixtures thereof.

8. The process according to any one of claims 1-6, wherein the hydrocarbon feed (B) comprises:(a) > 0.1 wt.% and < 90.0 wt.% of the decontaminated oligomeric product stream (DOS); and(b) > 10.0 wt.% and < 99.9 wt.% of the hydrocarbon stream (HD); with regard to the total weight of the hydrocarbon feed (B).

9. The process according to any one of claims 1-8, wherein the hydrocarbon stream (HD) is selected from heavy gas oil (HGO), light cycle oil (LCO), vacuum gas oil (VGO), atmospheric residue (AR), vacuum residue (VR), whole crude oil, cuts of crude oil, condensates, and mixtures thereof, preferably wherein the hydrocarbon stream (HD) is vacuum gas oil (VGO).

10. The process according to any one of claims 1-9, wherein the mechanical processing of the hydrocarbon feed (A) comprises at least one step selected from melt extrusion, compacting, mechanical agitation and any combinations thereof, preferably the mechanical processing of the hydrocarbon feed (A) comprises the step of melt extruding the hydrocarbon feed (A).

11. The process of claim 10, wherein the step of melt extruding the hydrocarbon feed (A) comprises the step of supplying the hydrocarbon feed (A) in a de-volatilization extruder; and extruding the hydrocarbon feed (A) under conditions of:(a) temperature of > 250 °C and < 450 °C, preferably > 300 °C and < 450 °C; and(b) a feed residence time of > 0.1 minute and < 60.0 minutes.

12. The process according to any one of claims 1-11, wherein the decontamination treatment comprises at least one process step selected from (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant hydrocarbon stream through a melt filter to obtain the decontaminated oligomeric product stream (DOS), (ii) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant stream, through a melt filter and subsequently through an adsorbent guard bed, preferably in the presence of hydrogen, to obtain the decontaminated oligomeric product stream (DOS), (iii) mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 350 °C followed by an alkaline treatment at a temperature of > 200 °C and < 350 °C prior to obtaining the decontaminated oligomeric product stream (DOS), (v) mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 430 °C, and passing the resultant stream, through a melt filter and subsequently over a de-metallization catalyst in presence of hydrogen to obtain the decontaminated oligomeric product stream (DOS), (vi) passing the oligomeric product stream (OS) over a de-metallization catalyst in presence of hydrogen, to obtain the decontaminated oligomeric product stream (DOS), and (vii) any combinations thereof.

13. The process according to claim 12, wherein the decontamination treatment comprises the steps of (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent at a temperature of > 200 °C and < 350 °C to obtain a stream (P) (ii) adding an aqueous alkali metal hydroxide solution to stream (P) at temperature of > 200 °C and < 350 °C to obtain an alkaline phase stream and a hydrocarbon phase stream, and (iii) separating the alkaline phase stream from the hydrocarbon phase stream to obtain the decontaminated oligomeric product stream (DOS); or the decontamination treatment of the oligomeric product stream (OS) comprises the step of (i) mixing the oligomeric product stream (OS) in a hydrocarbon solvent and passing the resultant hydrocarbon stream through a melt filter to obtain a filtrate stream (F); (ii) passing the filtrate stream (F), preferably in the presence of hydrogen, through a adsorbent guard bed at a temperature of > 200 °C and < 350 °C to obtain the decontaminated oligomeric product stream (DOS) after separating the hydrocarbon solvent.

14. The process according to any one of claims 1-13, wherein for an identical ratio of flow rate of hydrogen to the flow rate of hydrocracking feed (HF) and for an identical feed conversion, the hydrocracking feed (HF) is hydrocracked with lesser hydrogen consumption as compared to the hydrocracking of a similar hydrocracking feed which is not derived from the decontaminated oligomeric product stream (DOS).

15. A hydrocracking feed (HF) obtained according to the process of any one of claims 1-14, preferably wherein the hydrocracking feed (HF) has each of:(a) a total content of nickel and vanadium of < 150.0 parts per million (ppm) by weight, preferably < 100.0 parts per million (ppm) by weight, preferably < 50.0 parts per million (ppm) by weight, preferably < 15.0 parts per million (ppm) by weight, preferably < 5.0 parts per million (ppm) by weight; and(b) a total content of atomic sulfur of < 5.0 wt.%, preferably < 2.0 wt.%, with regard to the total weight of the hydrocracking feed (HF) as determined in accordance with ASTM D5453 (2012); and(c) a total content of atomic nitrogen of <3000 parts per million (ppm) by weight, preferably <500 parts per million (ppm) by weight, as determined in accordance with ASTM D5762 (2012); and(d) a silicon content of < 2.0 parts per million (ppm) by weight determined in accordance with ASTM D6130; and(e) a total olefinic content of < 5.0 wt.%, with regard to the total weight of the hydrocracking feed (HF).