Co-processing plastic pyrolysis oil to make high vi base oils and process fluids

Abstract

Disclosed are 2 cSt base stocks comprising a kinematic viscosity at 100°C of 1.5 cSt to 2.6 cSt, a saturates content of at least 90 wt. %, a sulfur content of less than 0.03%, a multicyclic naphthene content of 15 to 28 liquid volume %, a branching proximity of greater than 10, and a pour point of less than -30°C. Processes for making the base stocks and uses thereof are also disclosed.

Description

COPROCESSING PLASTIC PYROLYSIS OIL TO MAKE HIGH VI BASE OILS AND PROCESS FLUIDSCROSS-REFERENCE TO RELATED APPLICATIONS

[0001] This application claims the benefit of U.S. Provisional Application No. 63 / 716,895, filed on November 6, 2024, the entire contents of which are incorporated herein by reference.FIELD

[0002] The present disclosure relates to low viscosity base stock compositions, processes of making the same, and uses thereof.BACKGROUND

[0003] Of particular growing interest where superior performance would be of significant value are 2 cSt base oils, which are of increasing demand in low pour point applications such as transformer oils, low temperature hydraulic oils, automatic transmission fluids, data center cooling oils, and electric vehicle cooling oils.

[0004] To date, Group 11+ and Group III 2 cSt base oils have been produced from highly paraffinic stocks, such as through the isomerization of Fischer-Tropsch waxes (see, e.g., U.S. Patent No. 8,022,024) and slack wax. However, to meet the growing demand for these oils, it would be advantageous if they could be produced from other, less costly, sources. Furthermore, it would be even more advantageous if they could be produced in a way which benefits the environment and reduces the volume of plastic waste.

[0005] It would also be advantageous if a refiner could simply make a Group 11+ 2 cSt base oil by adding a minor amount of a different second feed to a lube oil feedstock ahead of a hydrocracking unit or an isomerization unit in order to boost viscosity index for as long as the Group 11+ 2 cSt base oil production was required. It would also be advantageous if a refiner could make a Group III 4 cSt base oil at the same time by boosting the viscosity index of 4 cSt base oil from Group II to Group III. It would also be beneficial if the second feed was low in cost.

[0006] One potential low-cost feed is waste plastics. Transforming waste plastic material and particularly polyethylene into useful products presents a unique opportunity to address a growing environmental problem.

[0007] Various processes for converting waste plastic into lubricating base oil have been developed. For example, U.S. Patent No. 6,150,577 discloses a process wherein wasteplastic is fed to a pyrolysis reactor. The pyrolysis effluent is separated into at least a heavy wax fraction which is hydrotreated and hydroisomerization dewaxed to form a high viscosity index (VI) lubricating base oil. U.S. Patent No. 8,404,912 discloses a process for making a high VI lubricating base oil which comprises hydrocracking a blend comprising a heavy wax derived from pyrolyzing a plastic feed and a lube oil feedstock, such as vacuum gas oil, in a lube hydrocracking zone to produce a hydrocracked stream and dewaxing at least a portion of the hydrocracked stream in a hydroisomerization zone to produce the base oil. U.S. Patent No. 8,480,880 discloses a process for making a lubricating base oil having a VI of at least 110 which comprises the steps of combining a waxy light neutral base oil and a wax derived from pyrolyzing a plastics feed comprising polyethylene to form a blend, hydroisomerization dewaxing the blend, and recovering the lubricating base oil from an effluent of the hydroisomerization dewaxing step. Of particular note is that these patents are directed at base oils of 3 cSt or higher.

[0008] According to the present disclosure, Applicant has found that adding a minor amount of a heavy waxy stream from a pyrolyzing a plastics feed to a petroleum feedstock can increase the 2 cSt fraction from a Group II to a Group 11+ base stock in which the content of multicyclic components (e.g., multi-ring naphthenes, multi-ring aromatics) is greater than 10 liquid volume percent, where multicyclic components have conventionally been known to negatively impact VI.SUMMARY

[0009] In a first aspect, the present disclosure relates to a base stock comprising: a kinematic viscosity at 100°C of 1.5 cSt to 2.6 cSt; a saturates content of at least 90 wt. %; a sulfur content of less than 0.03%; a multicyclic naphthene content of 15 to 28 liquid volume%; a branching proximity of greater than 10; and a pour point of less than -30°C.

[0010] In a second aspect, the present disclosure relates to a process for making a base stock, in particular a base stock as defined in the first aspect of the present disclosure, comprising the steps of (a) combining a waxy light neutral base stock and a pyrolysis oil originating from the pyrolysis of a plastics feed comprising polyethylene to form a combined feed; (b) hydroisomerization dewaxing the combined feed in a hydroisomerization zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent; and (c) recovering the base stock from the hydroisomerized effluent.

[0011] In a third aspect, the present disclosure relates to a process for making a base stock, in particular a base stock as defined in the first aspect of the present disclosure,comprising the steps of (a) providing a pyrolysis oil originating from the pyrolysis of a plastics feed comprising polyethylene, wherein the pyrolysis oil has a T99.5 cut point temperature in a range of from 480°C to 520°C; (b) providing a petroleum feedstock having a T5 to T95 boiling range of 316°C to 510°C; (c) combining the pyrolysis oil with the petroleum feedstock to form a combined feed, wherein the combined feed comprises 1 to 49 wt. % of pyrolysis oil relative to a combined weight of the pyrolysis oil and the petroleum feedstock; (d) hydrocracking the combined feed in a hydrocracking zone under hydrocracking conditions to produce a hydrocracked effluent; (e) separating the hydrocracked effluent into a gaseous fraction and a liquid fraction; (f) hydroisomerization dewaxing at least a portion of the liquid fraction in a hydroisomerization dewaxing zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent; and (g) recovering the base stock from the hydroisomerized effluent.

[0012] In a fourth aspect, the present disclosure relates to a fuel product prepared according to the process of the second or third aspect of the present disclosure.BRIEF DESCRIPTION OF THE DRAWINGS

[0013] FIG. l is a plot of viscosity index (VI) as a function of pour point for a 4 cSt oil obtained directly from dewaxing and hydrofinishing a hydrocracked LVGO and hydrocracked blends of pyoil and LVGO.

[0014] FIG. 2 is a plot of cloud point as a function of pour point for 4 cSt oil obtained directly from dewaxing and hydrofinishing a hydrocracked LVGO and hydrocracked blends of pyoil and LVGO.DETAILED DESCRIPTION

[0015] The present disclosure relates to low viscosity base stock compositions, processes of making the same, and uses thereof.Definitions

[0016] As used in this disclosure, the term “2 centistoke” or “2 cSt” interchangeably refers to any base stock or base oil having a kinematic viscosity at 100°C in a range of 1.5 cSt to 2.6 cSt with a sulfur content of less than 0.03%. With respect to kinematic viscosity, centistokes (cSt) and millimeter squared per second (mm2 / s) are equivalent CGS andSI units, respectively, representing a fluid’s resistance to flow under the influence of gravity. All kinematic viscosity values in this disclosure are as determined pursuant to ASTM D445. As used herein, “kinematic viscosity at 100°C” will be used interchangeably with “KV100” and “kinematic viscosity at 40°C” will be used interchangeably with “KV40.” The two terms should be considered equivalent.

[0017] As used in this disclosure, a “base stock” is a lubricant component that is produced by a single base stock manufacturer to the same specifications (independent of feed source or manufacturer’s location); that meets the same base stock manufacturer specification; and that is identified by a unique formula, product identification number, or both. As provided in Table 1 below, base stocks are categorized according to the American Petroleum Institute (API) classifications based on their saturated hydrocarbon content, sulfur level, and viscosity index. Typically, Group I, II, and III base stocks are each derived from crude oil via extensive processing, such as solvent extraction, solvent or catalytic dewaxing, and hydroisomerization. Group III base stocks can also be produced from synthetic hydrocarbon liquids obtained from natural gas, coal or other fossil resources. Group IV base stocks are polyalphaolefins (PAOs) and are produced by oligomerization of alpha olefins. Group V base stocks include all base stocks that do not belong to Groups I-IV, such as naphthenics, polyalkylene glycols (PAG), and esters.TABLE 1API Base Stock CategoriesAdditionally, there are the informal categories of base stocks referred to as “Group II+” and “Group III+” that are generally recognized within the lubricant industry as corresponding to base stocks that exceed the minimum classification requirements of the formal group. For example, a “Group II+” base stock can have a viscosity index (VI) of at least 110 and a “Group III+” base stock can have a viscosity index (VI) between 130 and 150.

[0018] Further, the base stocks may be referred to as light neutral (LN), medium neutral (MN), and heavy neutral (HN), for example, as determined by viscosity. The term “neutral” generally indicates the removal of most nitrogen and sulfur atoms to lower reactivity in the final oil. The base stocks are generally classified by viscosity, measured at 100°C as a kinematic viscosity under the techniques described in ASTM D445. The base oil stocks may also be classified by boiling point range, for example, determined by simulated distillation on a gas chromatograph, under the techniques described in ASTM D 2887. A “light neutral base oil stock” may have a kinematic viscosity of about 4 cSt to about 6 cSt and may have a boiling point range of about 380°C to about 450°C. A “medium neutral base oil stock” may have a kinematic viscosity of about 6 cSt to about 10 cSt and a boiling point range of about 440°C to about 480°C. A “heavy neutral base oil stock” may have a kinematic viscosity of about 10 cSt to about 20 cSt, or higher, and a boiling point range of about 450°C to about 565°C.

[0019] As used in this disclosure, the term “Cn hydrocarbons” or “Cn”, wherein “n” is a positive integer, is meant to describe all hydrocarbons having n carbon atoms. Moreover, the term “Cn+ hydrocarbons” or “Cn+” is meant to describe all hydrocarbon molecules having n or more carbon atoms. Accordingly, the term “Cn- hydrocarbons” or “Cn-” is meant to describe a mixture of hydrocarbons having n or less carbon atoms.

[0020] As used in this disclosure, the term “cut point” refers to the temperature on a True Boiling Point (TBP) curve at which a predetermined degree of separation is reached. “TBP” refers to the boiling point of a hydrocarbonaceous feed or product, as determined by Simulated Distillation (SIMDIST) by ASTM D2887.

[0021] As used in this disclosure, the term “effluent” refers to a stream that is passed out of a reactor, a reaction zone, or a separator following a particular reaction or separation process. Generally, an effluent has a different composition than the stream that entered the separator, reactor, or reaction zone. It should be understood that when an effluent is passed to another system unit, only a portion of that system stream may be passed. For example, a slip stream (having the same composition) may carry some of the effluent away, meaning that only a portion of the effluent may enter the downstream system unit. The term “reaction effluent” more particularly refers to a stream that is passed out of a reactor or reaction zone.

[0022] As used in this disclosure, the term “hydroprocessing” refers to a process in which a carbonaceous feedstock is brought into contact with hydrogen and a catalyst, at a higher temperature and pressure, for the purpose of removing undesirable impurities and / orconverting the feedstock to a desired product. Examples of hydroprocessing processes include hydrocracking, hydrotreating, catalytic dewaxing, and hydrofinishing.

[0023] As used in this disclosure, the term “hydrocracking” refers to a process in which hydrogenation and dehydrogenation accompanies the cracking / fragmentation of hydrocarbons, e.g., converting heavier hydrocarbons into lighter hydrocarbons, or converting aromatics and / or cycloparaffins (naphthenes) into non-cyclic branched paraffins.

[0024] As used in this disclosure, the term “hydroisomerization” refers to a process in which normal paraffins (n-alkanes) are isomerized to their more branched counterparts in the presence of hydrogen and over a hydroisomerization (dewaxing) catalyst. Hydroisomerization can improve one or more cold-flow properties of an isomerized fraction, such as viscosity, pour point and / or cloud point.

[0025] As used in this disclosure, the term “hydrofinishing” refers to a process that is intended to improve the oxidation stability, UV stability, and appearance of the hydrofinished product by removing traces of aromatics, olefins, color bodies, and solvents. As used in this disclosure, the term UV stability refers to the stability of the hydrocarbon being tested when exposed to UV light and oxygen. Instability is indicated when a visible precipitate forms, usually seen as floc or cloudiness, or a darker color develops upon exposure to ultraviolet light and air.

[0026] As used in this disclosure, the term “jet fuel” means hydrocarbons boiling in the range of a T10 between about 190°C (374°F) and about 215°C (419°F) and an end point of between about 290°C (554°F) and about 310°C (590°F).

[0027] As used herein, the term “multicyclic naphthene” means a saturated hydrocarbon having the general formula CnH2(n+i-r) arranged in the form of multiple closed rings, where n is the number of carbon atoms and r is the number of rings (here, r> 1).

[0028] As used in this disclosure, the terms “pyrolysis oil” and its abbreviated form “pyoil” are used herein to describe C10+ thermal cracking products having a pour point greater than 0°C, for example 10°C or more, or 20°C or more.

[0029] As used in this disclosure, the term “saturates” refers to all straight chain, branched, and cyclic paraffins. Thus, saturates correspond to a combination of paraffins and naphthenes.

[0030] As used in this disclosure, the term “sulfur” includes elemental sulfur and sulfur-containing compounds such as thiols, sulfides, thiophenes, benzo- and dibenzothiophenes, and more complex structures. Sulfur content may be determined in accordance with ASTM D1552, ASTM D2622, ASTM D3120, ASTM D4294 or ASTM D4927.

[0031] As used in this disclosure, the term “vacuum gas oil” (VGO) refers a byproduct of crude oil vacuum distillation that can be sent to a hydroprocessing unit or to an aromatic extraction for upgrading into base oils. VGO generally comprises hydrocarbons with a boiling range distribution of about 370°C to 550°C at 0.101 MPa.

[0032] As used in this disclosure, term “light vacuum gas oil” (LVGO) refer to hydrocarbons boiling in the range of about 370°C to 425°C, 370°C to 415°C, 370°C to 405°C, 370°C to 395°C, 380°C to 425°C, 390°C to 425°C, or 400°C to 425°C.

[0033] As used in this disclosure, the term “waxy” as refers to a feed having a high content of normal paraffins (n-paraffins). A waxy feed useful in the practice of the present process scheme will generally comprise at least 10 wt. % n-paraffins.

[0034] As used in this disclosure, the term “zone” refers to an area including one or more equipment, or one or more sub-zones. Equipment may include one or more reactors or reactor vessels, heaters, heat exchangers, pipes, pumps, compressors, and controllers. Additionally, an equipment, such as dryer, or vessels, further may be included in one or more zones.

[0035] “ Cloud point” refers to the temperature at which paraffin wax or other solid components start to precipitate from a petroleum product, causing it to become cloudy or hazy. Cloud point may be determined in accordance with ASTM D5773.

[0036] “Pour point” is the temperature at which a liquid no longer flows. Pour point may be determined in accordance with ASTM D97.

[0037] “Viscosity index” (VI) is a measure of the extent of viscosity change with temperature; the higher the VI, the less change, and generally speaking, higher Vis are preferred. VI is usually calculated from measurements at 40°C and 100°C. Viscosity index is an empirical, unitless number which indicates the rate of change in the viscosity of an oil within a given temperature range. Fluids exhibiting a relatively large change in viscosity with temperature are said to have a low viscosity index. A low VI oil, for example, will thin out at elevated temperatures faster than a high VI oil. Usually, a high VI oil is more desirable becauseit has higher viscosity at higher temperature, which translates into better or thicker lubrication film and better protection of the contacting machine elements. Viscosity index may be determined in accordance with ASTM D2270.

[0038] “Wax content” - To determine the true wax content of an oil, the oil sample was solvent dewaxed with methyl ethyl ketone at -15°C to precipitate the “wax”. There is usually still some oil in the “wax” resulting from the solvent dewaxing process. ASTM D721 is used to quantify this additional amount of oil, and this value is subtracted from the “wax” weight to determine the true wax content in the original oil sample.

[0039] As used in this disclosure, the term “branching index” (BI) is the percentage of methyl hydrogens appearing in the chemical shift range of 0.5 to 1.05 ppm among all hydrogens appearing in theJH NMR chemical range 0.5 to 2.1 ppm in an isoparaffinic hydrocarbon.

[0040] As used in this disclosure, the term “branching proximity” (BP) refers to the percentage of recurring methylene carbons which are four or more number of carbon atoms removed from an end group or branch (epsilon-CTb carbons) appearing at13C NMR chemical shift 29.8 ppm.

[0041] As used in this disclosure, the term “methyl branches per molecule” is the number that includes 2-methyl, 3 -methyl, 4-methyl, 5+ methyl, adjacent methyl, and unknown methyl appearing between13C NMR chemical shift 0.5 ppm and 22.0 ppm, except end methyl carbons appearing at 13.8 ppm.

[0042] As used in this disclosure, the term “free carbon index” is the average number of methylene carbons which are four or more number of carbon atoms removed from an end group or branch (epsilon-CTb carbons) per molecule. Some characteristic13C NMR chemical shift assignments are reported in Table 2:TABLE 2For the assignment of the various branch carbon resonances to specific branch positions and lengths using tabulated and calculated values see, e.g., L.P. Lindeman etal. (Anal. Chem. 1971, 43, 1245-1252) and D.A. Netzel et al. (Fuel, 1981, 60, 307-320).Base Stock

[0043] In a first aspect, the present disclosure relates to a base stock comprising: a kinematic viscosity at 100°C of 1.5 cSt to 2.6 cSt; a saturates content of at least 90 wt. %; a sulfur content of less than 0.03%; a multicyclic naphthene content of 15 to 28 liquid volume %; a branching proximity of greater than 10; and a pour point of less than -30°C.

[0044] In some embodiments, the base stock can have a kinematic viscosity at 100°C of in a range of 2.0 cSt to 2.6 cSt, such as 2.0 cSt to 2.5 cSt, or 2.0 cSt to 2.4 cSt, or 2.1 cSt to 2.6 cSt, or 2.1 cSt to 2.5 cSt, or 2.1 cSt to 2.4 cSt, or 2.2 cSt to 2.6 cSt, or 2.2 cSt to 2.5 cSt, or 2.2 cSt to 2.4 cSt.

[0045] With regard to saturates, the base stock can in some embodiments have a total saturates content, as measured by ASTM D7419 or ASTM D2007, of 92 wt. % or more, 94 wt. % or more, 96 wt. % or more, or 98 wt. % or more. Due to the high content of saturates, the amount of aromatics is correspondingly low.

[0046] In some embodiments, the base stock can have a multicyclic naphthene content of 20 to 28 liquid volume % (LV%), such as 20 to 25 liquid volume %.

[0047] In some embodiments, the base stock can have an NMR branching proximity of greater than or equal to 11, greater than or equal to 12, greater than or equal to 13, or greater than or equal to 14.

[0048] In some embodiments, the base stock can have a pour point of-35°C or less, or -40°C or less, and / or down to any convenient low pour point value, such as -60°C or even lower.

[0049] In some further embodiments, the base stocks can be an API Group 11+ base stock.

[0050] In some further embodiments, the base stock can have a viscosity index of 110 to 119, such as 113 to 119, or 115 to 119.Processes for Making a Base Stock

[0051] In a second aspect, the present disclosure relates to a process for making a base stock, in particular a base stock as defined in the first aspect of the present disclosure, comprising the steps of (a) combining a waxy light neutral base stock and a pyrolysis oil originating from the pyrolysis of a plastics feed comprising polyethylene to form a blend; (b) hydroisomerization dewaxing the blend in a hydroisomerization zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent; and (c) recovering the base stock from the hydroisomerized effluent.

[0052] In some embodiments, the waxy light neutral base stock for co-processing with the pyrolysis oil can correspond to any conventional waxy light neutral base stock. In some embodiments, the waxy light neutral base stock is a hydrocracked waxy light neutral base stock. In some embodiments, the waxy light neutral base oil has a pour point of at least 20°C, for example, 20°C to 40°C, 20°C to 30°C, or 20°C to 24°C.

[0053] Suitably, the waxy light neutral base stock utilized in the present process scheme has low levels of nitrogen and sulfur, for example less than 25 ppm total combined nitrogen and sulfur and often less than 10 ppm.

[0054] The pyrolysis oil of the present disclosure is obtained via the pyrolysis of a plastics feed, typically waste plastic. The pyrolysis of plastics is well known in the art, and may involve a catalytic or non-catalytic process, in a continuous or batch process.

[0055] The plastics feed for the pyrolysis process may comprise a mixture of different types of plastic. Preferred plastic types include high-density polyethylene (HDPE), low-density polyethylene (LDPE), and polypropylene (PP) and their polyolefin copolymers. However, also other plastic types may be present, such as polyethylene terephthalate (PET or PETE) andpolystyrene (PS). In some embodiments, the plastics feed comprises at least 10 wt. %, at least 50 wt. %, or at least 90 wt. % polyethylene.

[0056] The pyrolysis oil includes typically one or more hydrocarbon materials selected from paraffins, olefins, naphthenes, and aromatics. The relative amount of these components may depend on the specific pyrolysis process conditions and the plastic material.

[0057] The pyrolysis oil may comprise a C10+ stream (e.g., a C10-C35 stream, a C10- C30 stream, a C20-C35 stream, or a C20-C30 stream). The pyrolysis oil may comprise 50 wt. % or more (e.g., 50 to 100 wt. %, or 50 to 75 wt. %, or 70 to 90 wt. %, or 80 to 100 wt. %) of C10+ hydrocarbons and less than 50 wt. % (e.g., 0 to less than 50 wt. %, or 25 to 50 wt. %, or 10 to 30 wt. %, or 0 to 20 wt. %, or 0 to 5 wt. %, or 0 to 2 wt. %) of C9- hydrocarbons.

[0058] Certain properties of the pyrolysis oil may be desirable in the processes disclosed herein. For example, in some embodiments, the pyrolysis oil fraction can be characterized by any one or any combination of more than one of the following properties:• an API gravity of 25 to 65, 25 to 50, 30 to 70, 50 to 75, or 30 to 65, or any range therebetween;• a wax content in the range of 30 to 90 wt. %, or 30 to 80 wt. %, or 20 to 70 wt. %, or 20 to 60 wt. %, or 20 to 50 wt. %, or 20 to 40 wt. %, or 20 to 30%, or at least 10 wt. %, or at least 20 wt. %, or at least 30 wt. %, or at least 35 wt. %, or at least 40 wt. %, or any range between two of these recited values;• a pour point of 10°C or more, 20°C or more, 30°C or more, 40°C or more, or any range between two of these recited values;• a nitrogen content of 500 ppm or less, 400 ppm or less, 300 ppm or less, 200 ppm or less, 100 ppm or less, or 50 ppm or less, or any range between two of these recited values• a sulfur content of 200 ppm or less, 100 ppm or less, 50 ppm or less, or 25 ppm or less, or any range between two of these recited values;• a chlorine content of 10 ppm or less, or 5 ppm or less;• a boiling range of 500°F to 950°F (260°C to 510°C) or 500°F to 750°F (260°C to 399°C).

[0059] The pyrolysis oil may be pre-processed, for example, to reduce or remove one or more contaminants. Contaminants may include one or more of Cl, P, Al, Ca, Fe, Mg, Na, Ti, and Si, which can negatively impact downstream catalysts and equipment.

[0060] In some particular embodiments, the waxy light neutral base stock and the pyrolysis oil are mixed to form a combined feed prior to entering the hydroisomerization dewaxing zone. In other embodiments, the waxy light neutral base stock and the pyrolysis oil are separately introduced into the hydroisomerization dewaxing zone. More generally, however, any convenient method for introducing both the waxy light neutral base oil and the pyrolysis oil into the hydroisomerization dewaxing zone can be used.

[0061] Prior to being introduced into the hydroisomerization dewaxing zone, the feedstocks (optionally in the form of a combined feed) are pre-heated in accordance with one or more embodiments. For example, a pyrolysis oil and a petroleum feedstock can be mixed in a heated stirred tank for storage operating at 200°C to 325°C or 275°C to 325°C.

[0062] In a combined feed, any convenient ratio of waxy light neutral base stock to pyrolysis oil can be used, so long as the weight of waxy light neutral base stock is greater than the weight of pyrolysis oil. In various aspects, relative to the combined weight of waxy light neutral base stock and pyrolysis oil, the waxy light neutral base stock can correspond to 51 to 99 wt. % of the combined weight, or 70 to 99 wt. %, or 51 to 90 wt. %, or 70 to 90 wt. %, or 70 to 85 wt. %, or 70 to 80 wt. %. Therefore, the weight of pyrolysis oil can correspond to 1 to 49 wt. % of the combined weight of waxy light neutral base stock and pyrolysis oil, or 1 to 30 wt. %, or 10 to 49 wt. %, or 10 to 30 wt. %, or 15 to 30 wt. %, or 20 to 30 wt. %. Addition of pyrolysis oil can decrease the yield of the finished oil at the target pour point. The higher wax content of the pyrolysis oil may require more severe process conditions to meet the target pour point. Thus, the amount of pyrolysis oil in the blend may need to be limited to meet the target pour point.

[0063] It is usually desirable to maintain as low a cloud point as possible for the combined feed. Consequently, a fraction of pyrolysis oil may be used to produce low-viscosity base stocks. The fraction can have a T99.5 cut point temperature in a range of from about 480°C to 520°C, such as about 510°C. Without wishing to be bound by any theory, it is believed that removal of the heavy fraction boiling above 520°C from the pyrolysis oil can result in higher quality base stock with reduced pour / cloud spread and / or haze in the base stocks produced according to the present disclosure.

[0064] The combined feed is subsequently dexawed in a hydroisomerization dewaxing zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent.

[0065] In an embodiment, dewaxing processes of the present disclosure use a hydroisomerization catalyst selective for the isomerization of n-paraffins in the feed, such thatfeedstock components are preferentially isomerized rather than cracked. The hydroisomerization catalyst may comprise a medium-pore 1 -dimensional, 10-membered oxygen ring molecular sieve and a Group 8-10 metal. Representative examples of molecular sieves that may be useful in formulating hydroisomerization catalysts include SAPO-11, SM- 3, SAPO-41, SSZ-32, SSZ-91, ZSM-11, ZSM-22, ZSM-23, ZSM-35, and ZSM-48. The Group 8-10 metal of the hydroisomerization catalyst may comprise platinum, palladium, or a combination thereof. In an embodiment, the hydroisomerization catalyst may comprise from 0.1 to 1.5 wt. % of the Group 8-10 metal, typically from 0.2 to 1.0 wt. %, and usually from 0.325 to 1.0 wt. % of the Group 8-10 metal.

[0066] In an embodiment, the hydroisomerization catalyst may further comprise a metal modifier selected from the group consisting of Mg, Ca, Sr, Ba, K, La, Pr, Nd, Cr, and combinations thereof. In an embodiment, a metal-modified catalyst of the present disclosure may comprise from 0.5 to 3.5 wt. % of Mg or other metal modifier(s), typically from 0.5 to 2.5 wt. %, and usually from 0.9 to 2.5 wt. % of Mg or other metal modifier(s).

[0067] Typically, the hydroisomerization catalyst will still further comprise a support or binder. The support may comprise a refractory inorganic oxide. Suitable inorganic oxide supports for the hydroisomerization catalyst can include silica, alumina, titania, magnesia, zirconia, silica-alumina, silica-magnesia, silica-titania, and the like, and combinations thereof. The hydroisomerization catalyst may comprise from 5 to 95 wt. % or more of the molecular sieve component, typically from 15 to 85 wt. % of the molecular sieve, and usually from a 25 to 75 wt. % of the molecular sieve. Generally, it is advantageous to minimize the molecular sieve component for economic reasons, provided that the catalyst retains the required activity and selectivity levels. The hydroisomerization catalyst may comprise from about 0 to 95 wt. % of the support material, and more typically from 5 to 90 wt. %.

[0068] Hydroisomerization dewaxing conditions generally depend on the feed used, the catalyst used, desired yield, and the desired properties of the base stock. Process conditions in a hydroisomerization dewaxing zone can include a temperature of 550°F to 700°F (288°C to 371°C), such as 590°F to 675°F (310°C to 357°C); a pressure of 15 psig to 3000 psig (0.10 MPa to 20.68 MPa gauge), such as 100 psig to 2500 psig (6.89 MPa to 17.24 MPa gauge); a liquid hourly space velocity (LHSV) of 0.1 h'1to 20 h’1, such as 0.1 h'1to 5 h’1; and a hydrogen- to-hydrocarbon ratio of 2000 to 10,000 standard cubic feet per barrel hydrocarbon feed (356 to1781 m3Jfc / m3feed), such as 2500 to 5000 standard cubic feet per barrel hydrocarbon feed (445 to 891 m3Jfc / m3feed).

[0069] The hydroisomerized effluent can be fractionated, notably by distillation, to recover one or more base stock products. For example, lubricant base stock products can be recovered corresponding to a 2 cSt cut, a 3 cSt cut, a 4 cSt cut, a 6 cSt cut, and / or a cut having a viscosity higher than 6 cSt. For example, a 2 cSt cut fraction (e.g., KV100 = 1.5 to 2.6 cSt) can be a fraction suitable for use in low pour point applications such as transformer oils, low temperature hydraulic oils, or automatic transmission fluids. A 4 cSt cut fraction (e.g., KV100 = 3.5 to 4.5 cSt) can be a fraction having a controlled volatility and low pour point, such that the fraction is suitable for engine oils made according to SAE J300 in 0W- or 5W- or 10W- grades.

[0070] In addition to the various base stock products, a fuel product may also be recovered by fractionation of the hydroisomerized effluent. In one embodiment, a jet fuel fraction is recovered. The recovered jet fuel fraction can be used as a jet fuel and / or a jet fuel component. Since the jet fuel fraction produced in accordance with the processes of the present disclosure is derived at least in part from a waste plastics source, at least a portion of the material may be claimed as a sustainable jet fuel and / or jet fuel component.

[0071] In various aspects, a hydrofinishing process can also be provided. The hydrofinishing can occur prior to dewaxing and / or after dewaxing. The hydrofinishing can occur either before or after fractionation. If hydrofinishing occurs after fractionation, the hydrofinishing can be performed on one or more portions of the fractionated product, such as being performed on one or more lubricant base stock portions. Alternatively, the entire effluent from the dewaxing process can be hydrofinished.

[0072] Hydrofinishing conditions can include a temperature of 350°F to 650°F (176°C to 343°C), a pressure of 400 psig to 4000 psig (2.76 to 27.58 MPa gauge), and a liquid hourly space velocity of 0.1 h'1to 5 h’1.

[0073] Hydrofinishing catalysts can include catalysts containing Group 6 metals, Group 8-10 metals, and mixtures thereof. In an embodiment, preferred metals include at least one metal sulfide having a strong hydrogenation function. In another embodiment, the hydrofinishing catalyst can include a Group 8-10 noble metal, such as Pt, Pd, or a combination thereof. Suitable metal oxide supports include low acidic oxides such as silica, alumina, silica- alumina or titania, notably alumina.

[0074] In a third aspect, the present disclosure relates to a process for making a base stock, in particular a base stock as defined in the first aspect of the present disclosure, comprising the steps of (a) providing a pyrolysis oil originating from the pyrolysis of a plastics feed comprising polyethylene, wherein the pyrolysis oil has a T99.5 cut point temperature in a range of from 480°C to 520°C; (b) providing a petroleum feedstock having a T5 to T95 boiling range of 316°C to 510°C; (c) combining the pyrolysis oil with the petroleum feedstock to form a combined feed, wherein the combined feed comprises 1 to 49 wt. % of pyrolysis oil relative to a combined weight of the pyrolysis oil and the petroleum feedstock; (d) hydrocracking the combined feed in a hydrocracking zone under hydrocracking conditions to produce a hydrocracked effluent; (e) separating the hydrocracked effluent into a gaseous fraction and a liquid fraction; (f) hydroisomerization dewaxing at least a portion of the liquid fraction in a hydroisomerization dewaxing zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent; and (g) recovering the base stock from the hydroisomerized effluent.

[0075] A wide variety of petroleum feedstocks can be used, including whole crude petroleum, reduced crudes, vacuum tower residua, synthetic crudes, foots oils, Fischer-Tropsch derived waxes, and the like. Typical feedstocks can include hydrotreated or hydrocracked gas oils, hydrotreated lube oil raffinates, bright stocks, lubricating oil stocks, synthetic oils, foots oils, Fischer-Tropsch synthesis oils, high pour point polyolefins, normal alpha olefin waxes, slack waxes, deoiled waxes and microcrystalline waxes. Other hydrocarbon feedstocks suitable for use in processes of the present process scheme may be selected, for example, from gas oils and vacuum gas oils, residuum fractions from an atmospheric pressure distillation process, solvent deasphalted petroleum residua, shale oils, cycle oils, petroleum and slack wax, and waxes produced in chemical plant processes. In some embodiments a petroleum feedstock can correspond to a mineral feedstock, such as a feedstock comprising at least 50 wt. % of feed derived from a mineral source, or at least 75 wt. %, or at least 95 wt. %.

[0076] One way of defining a feedstock is based on the boiling range of the feed. One option for defining a boiling range is to use an initial boiling point for a feed and / or a final boiling point for a feed. Another option is to characterize a feed based on the amount of the feed that boils at one or more temperatures. For example, a “T5” boiling point / distillation point for a feed is defined as the temperature at which 5 wt. % of the feed will boil off. Similarly, a “T95” boiling point / distillation point is a temperature at 95 wt. % of the feed will boil. Boiling points, including fractional weight boiling points, can be determined using a suitable ASTM method such as the procedures described in ASTMD86, D2887, D2892, D6352, and / or D7129.

[0077] Typical feeds include, for example, feeds with an initial boiling point and / or a T5 boiling point and / or T10 boiling point of at least 600°F (316°C), or at least 650°F (343°C), or at least 700°F (371°C), or at least 750°F (399°C). Additionally or alternately, the final boiling point and / or T95 boiling point and / or T90 boiling point of the feed can be 1100°F (593°C) or less, or 1050°F (566°C) or less, or 1000°F (538°C) or less, or 950°F (510°C) or less. In particular, a feed can have a T5 to T95 boiling range of 600°F (316°C) to 1100°F (593°C), or a T5 to T95 boiling range of 600°F (316°C) to 950°F (510°C), or a T10 to T90 boiling range of 600°F (316°C) to 950°F (510°C).

[0078] Certain properties of the petroleum feedstock may be desirable in the processes disclosed herein. For example, in an aspect, the petroleum feedstock can be characterized by any one or any combination of more than one of the following properties:• an API gravity in the range of 15 to 40, or 15 to 30, or 15 to 25, or greater than or equal to 15, or greater than or equal to 17;• a viscosity index in the range of 30 to 90, or 40 to 90, or 50 to 90, or 60 to 90;• a kinematic viscosity at 100°C (KV100) in the range of 3 to 30 cSt, or 3 to 20 cSt, or 3 to 10 cSt, or 3 to 15 cSt, or about 5 cSt;• a wax content in the range of 5 to 90 wt. %, or 5 to 80 wt. %, or 5 to 70 wt. %, or 5 to 60 wt. %, or 5 to 50 wt. %, or 5 to 40 wt. %, or 5 to 30 wt. % or 5 to 20 wt. %, or >5 wt. %, or >10 wt. %, or >15 wt. %;• a nitrogen content of 1500 ppm or less, or 1000 ppm or less, 500 ppm or less, or in the range of 50 to 1500 ppm, or 50 to 1000 ppm, or 50 to 500 ppm;• a sulfur content of 4000 ppm or less, or 3000 ppm or less, or 2000 ppm or less, or 1000 ppm or less, or in the range of 100 to 4000 ppm, or 100 to 3000 ppm, or 100 to 2000 ppm, or 100 to 1000 ppm; and / or• a 1050°F+ (565.6°C+) content of 10 wt. % or less, or <5 wt. %, or 2 wt. % or less, or in the range of 1 to 10 wt. % or 1 to 5 wt. %.

[0079] In some embodiments, the petroleum feedstock comprises vacuum gas oil, or consists essentially of vacuum gas oil, or consists of vacuum gas oil, including whole uncut feedstocks and cut feedstocks. In particular embodiments, the vacuum gas oil is a light vacuum gas oil (LVGO).

[0080] In embodiments, the pyrolysis oil and the petroleum feedstock can be mixed to form a combined feed prior to entering the hydrocracking zone. More generally, any convenientmethod for introducing both the pyrolysis oil and the petroleum feedstock into the hydrocracking zone can be used.

[0081] Prior to being introduced into the hydrocracking zone, the feedstocks (optionally in the form of a combined feed) are pre-heated. Pre-heating the feedstocks in one or more heating stages can increase the temperature of the feedstocks to a mixing and storage temperature, to a temperature related to the hydrocracking temperature, or to another convenient temperature.

[0082] In some embodiments, a portion of the pre-heating of a pyrolysis oil can be performed by mixing the pyrolysis oil with a petroleum feedstock in a mixing tank and heating the mixture in the mixing tank. For example, a pyrolysis oil and a petroleum feedstock can be mixed in a heated stirred tank for storage operating at 200°C to 325°C, or 275°C to 325°C.

[0083] In a combined feed, any convenient ratio of petroleum feedstock to pyrolysis oil can be used, so long as the weight of petroleum feedstock is greater than the weight of pyrolysis oil. In various aspects, relative to the combined weight of petroleum feedstock and plastic- derived pyrolysis oil, the petroleum feedstock can correspond to 51 to 99 wt. % of the combined weight, or 70 to 99 wt. %, or 51 to 90 wt. %, or 70 to 90 wt. %, or 70 to 85 wt. %, or 70 to 80 wt. %. Therefore, the weight of pyrolysis oil can correspond to 1 to 49 wt. % of the combined weight of petroleum feedstock and pyrolysis oil, or 1 to 30 wt. %, or 10 to 49 wt. %, or 10 to 30 wt. %, or 15 to 30 wt. %, or 20 to 30 wt. %.

[0084] The combined feed is contacted with a hydrocracking catalyst in a hydrocracking zone under hydrocracking conditions to provide a hydrocracked effluent.

[0085] Process conditions in a hydrocracking zone can include a temperature of 450°F to 900°F (232°C to 482°C), for example, 650°F to 850°F (343°C to 454°C); a pressure of 500 psig to 5000 psig (3.45 MPa to 34.5 MPa gauge), for example, 1500 psig to 3500 psig (10.34 MPa to 24.13 MPa gauge); a liquid hourly space velocity (LHSV) of 0.1 h1to 15 h for example, 0.25 h1to 2.5 h and a hydrogen consumption of 500 to 2500 standard cubic feet per barrel of liquid hydrocarbon feed (89 to 445 m3Fb / m3feed).

[0086] The hydrocracking may utilize any suitable hydrocracking catalyst or configuration known in the art. Generally, such catalysts include a hydrogenation metal component and an acidic support component. In certain embodiments, the hydrocracking catalyst may include one or more of the group consisting of amorphous alumina catalysts, amorphous silica alumina catalysts, natural or synthetic zeolite-based catalysts. The hydrocracking catalyst can possess one or more metals selected from the group consisting ofPt, Pd, Ni, W, Mo, and Co. In particular embodiments, acidic alumina or silica-alumina based supported catalysts that comprise Ni and one or more of Mo and W may be used.

[0087] The hydrocracking process may be a single- or a multi-stage process.

[0088] The hydrocracked effluent from the hydrocracking zone may comprise H2, impurity products (e.g., H2S and NH3), light ends (C1-C4 hydrocarbons and naphtha), distillate fuel range hydrocarbons (e.g., jet, diesel) and hydrocarbons boiling above the distillate fuel range.

[0089] The step of separating the hydrocracked effluent into a gaseous fraction and a liquid fraction may be performed by means of any separating devices known to those skilled in the art, such as one or more separating drums, which may operate at different pressures and temperatures, optionally in combination with a hydrogen or steam stripping means and with one or more distillation columns. These separators can, for example, be high-pressure high- temperature (HPHT) separators and / or high-pressure low-temperature (HPLT) separators.

[0090] The gaseous fraction obtained at the end of the separating comprises gases, such as H2, H2S, NH3, any light gases including C1-C4 hydrocarbons, and any naphtha.

[0091] The liquid fraction obtained at the end of the separating comprises distillate fuel range hydrocarbons and a bottom fraction comprising hydrocarbons boiling above the distillate fuel range hydrocarbons.

[0092] At least a portion of liquid fraction of the hydrocracked effluent is passed to a hydroisomerization dewaxing zone where the hydrocracked effluent is subjected to hydroisomerization dewaxing conditions to produce a hydroisomerized effluent. Hydroisomerization dewaxing conditions are as described herein above.

[0093] The hydroisomerized effluent can be fractionated, notably by distillation, to recover one or more base stock products. For example, lubricant base stock products can be recovered corresponding to a 2 cSt cut, a 3 cSt cut, a 4 cSt cut, a 6 cSt cut, and / or a cut having a viscosity higher than 6 cSt.

[0094] In addition to the various base stock products, a fuel product may also be recovered by fractionation of the hydroisomerized effluent. In one embodiment, a jet fuel fraction is recovered. The recovered jet fuel fraction can be used as a jet fuel and / or a jet fuel component. Since the jet fuel fraction produced in accordance with the processes of the present disclosure is derived at least in part from a waste plastics source, at least a portion of the material may be claimed as a sustainable jet fuel and / or jet fuel component.

[0095] In various aspects, a hydrofinishing process can also be provided, as discussed hereinabove.Uses

[0096] The base stocks described herein can also be blended with other base stocks to make a base oil. These other base stocks include Group I, III, IV and V base stocks and gas-to- liquid (GTL) oils. These base oil blends of the present base stock and other base stocks can also be combined with additives to make formulated lubricants. The base stocks described herein are well suited as lube base stocks without blending limitations, and further, the lube base stock products are also compatible with lubricant additives for lubricant formulations.

[0097] The lube base stocks of the present disclosure can be used in a variety of lubricant-related end uses, such as a lubricant oil for a device or apparatus requiring lubrication of moving and / or interacting mechanical parts, components, or surfaces. Useful apparatuses include engines and machines. The 2 cSt base stocks of the present disclosure are particularly suitable for use in the formulation of transformer oils, low temperature hydraulic oils, automatic transmission fluids, data center cooling oils, and electric vehicle cooling oils. The 4 cSt base stocks of the present disclosure are particularly suitable for use in the formulation of advanced engine oils, industrial lubricants, and heat transfer fluids.EXAMPLES

[0098] Aspects of the disclosure are described in greater detail by way of specific examples. The following examples are offered for illustrative purposes and are not intended to limit the disclosure in any manner. Those of skill in the relevant art will readily recognize a variety of parameters can be changed or modified to yield essentially the same results.EXAMPLE 1Feeds for Hydroprocessing

[0099] Table 3 shows the properties of light vacuum gas oil (LVGO) and pyrolysis oil / LVGO feeds used for this study. Two blends containing 20 vol% and 28 vol% pyrolysis oil with LVGO were prepared as hydrocracker feeds for testing.TABLE 3Hydrocracker Feed Properties

[0100] As received pyrolysis oil was distilled to remove the heavy end (about 950°F cut point) as taught by U.S. Patent No. 8,480,880. LVGO and the two pyoil / LVGO blends were processed in a lab hydrocracker unit, all at about a reaction temperature of 690°F, a liquid hourly space velocity (LHSV) of 0.55 h’1, a total pressure of 2100 psig, a recycle gas rate of about 4400 SCF / B.

[0101] The heavy portion of the hydrocracked product streams (about 540°F+) was subsequently dewaxed and hydrofinished by conventional means in a lab unit.EXAMPLE 22 cSt Base Stocks

[0102] The process of the present disclosure makes excellent quality 2 cSt base stocks. Table 4 below shows a comparison between a commercial light base oil of about 2 cSt KV100 and the final 2 cSt base stock product of the process in Example 1.TABLE 4Properties of 2 cSt Base Stocks

[0103] The data in Table 4 show that pyoil coprocessing at 20 vol% produces excellent VI 2 cSt base stock. With the pyoil coprocessing, the base stock quality has lifted from Group II to Group II+, as the result of a 15 number improvement in VI.EXAMPLE 3Analysis of 2 cSt Base Stocks

[0104] A 2 cSt base stock prepared according to Example 1 from the 20% pyoil / LVGO feed and a commercial 2 cSt base stock were analyzed byJH NMR and13C NMR analysis. The results are presented in Table 5.TABLE SNMR Analysis

[0105] Table 5 shows that the pyoil / LVGO blend produced a 2 cSt base stock with a lower branching index than LVGO only (28.9 vs. 32.3) and a higher branching proximity (14.1 vs 9.0) than LVGO only. Without being bound by any particular theory, it is believed that the higher branching proximity and lower branching index contributes to the surprising gain in VI at the target pour point. This suggests a significant benefit when the branching proximity is greater than 10, more preferably greater than 12.

[0106] The 2 cSt base stocks were also analyzed for hydrocarbon-type by 22x22 mass spectrometry, with the results given in Table 6. Hydrocarbon-type analysis was performed using a high-resolution magnetic mass spectrometer with the magnet scanned from 40 to 500 Daltons.TABLE 6 Component Analysis

[0107] Table 6 shows that the base stock prepared from pypoil / LVGO has a much higher paraffin content than commercial 2 cSt oil. It also has a multicyclic naphthene content of 22.8 liquid volume percent (LV%), unexpectedly high for a Group 11+ oil.EXAMPLE 44 cSt Base Stocks

[0108] Each of the hydrocarbon products from Example 1 was distilled to produce a 4 cSt base stock fraction.

[0109] FIG. l is a plot of viscosity index (VI) as a function of pour point for 4 cSt base stock obtained directly from dewaxing and hydrofinishing a hydrocracked LVGO, and hydrocracked blends of pyoil and LVGO. The results show that the 4 cSt base oil products made from 20% and 28% feed blends have significantly higher viscosity index (in the range of 120 to 126 VI depending on the pour point) while the base oil made from 100% LVGO showed 114-116 VI . The use of pyoil blends enables the production of Group III base oil (VI > 120 at -15°C pour point) while LVGO only produced a Group II base oil (VI <120 at -15°C pour point). These Group III targets are unattainable with the 100% LVGO of Example 1.

[0110] FIG. 2 is a plot of cloud point as a function of pour point for base stock obtained directly from dewaxing and hydrofinishing a hydrocracked LVGO and hydrocracked blends of pyoil and LVGO. The results show that the products made with pyoil blend show about the same pour / cloud spread as the commercial 100 N (100% LVGO) case.

[0111] Table 7 summarizes the overall yields from the various feeds (100% LVGO, 20% cut pyoil / LVGO, 28% cut pyoil / LVGO).TABLE 74 cSt Base Stock PropertiesEXAMPLE 5Jet Fuels

[0112] Each of the hydrocarbon products from Example 1 was distilled to produce a jet fuel fraction and analyzed for jet fuel properties. The results are summarized in Table 8.Table 8Properties of Jet Fraction

[0113] The results in Table 8 indicate that co-processing of pyoil with LVGO by hydrocracking makes an excellent jet fuel blending component. Since the feedstocks of the pyoil / LVGO blend were made from a waste plastic source, the jet fuel produced by this route contains sustainable material and the carbon intensity may be lower than the corresponding jet fuel made from LVGO only.

Claims

CLAIMS1. A base stock comprising: a kinematic viscosity at 100°C of 1.5 cSt to 2.6 cSt; a saturates content of at least 90 wt. %; a sulfur content of less than 0.03%; a multi cyclic naphthene content of 15 to 28 liquid volume %; a branching proximity of greater than 10; and a pour point of less than -30°C.

2. The base stock of claim 1, wherein the base stock composition has a kinematic viscosity at 100°C of2.0 cSt to 2.6 cSt.

3. The base stock of claim 1, wherein the base stock has a saturates content of 96 wt. % or more.

4. The base stock of claim 1, wherein the base stock has a viscosity index of 110 to 119.

5. The base stock of claim 1, wherein the base stock has a viscosity index of 113 to 119.

6. The base stock of claim 1, wherein the base stock has a multi cyclic naphthene content of 20 to 28 liquid volume %.

7. The base stock of claim 1, wherein the base stock has a branching proximity of greater than 12.

8. The base stock of claim 1, wherein the base stock has a pour point of -40°C to -60°C.

9. A process for making a base stock, the process comprising:(a) combining a waxy light neutral base stock and a pyrolysis oil originating from the pyrolysis of a plastics feed comprising polyethylene to form a combined feed;(b) hydroisomerization dewaxing the combined feed in a hydroisomerization zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent; and(c) recovering from the hydroisomerized effluent the base stock of claim 1.

10. The process of claim 9, wherein the waxy light neutral base stock has a normal paraffins content of at least 10 wt. %.

11. The process of claim 9, wherein the waxy light neutral base stock has a kinematic viscosity at 100°C of 4 cSt to 6 cSt and a boiling point range of 380°C to 450°C.

12. The process of claim 9, wherein the waxy light neutral base oil has a combined total nitrogen and sulfur content of less than 25 ppm.

13. The process of claim 9, wherein the pyrolysis oil is characterized by one or any combination of more than one of the following properties: an API gravity of 25 to 65; a wax content of 10 to 90 wt. %; a nitrogen content of 500 ppm or less; a sulfur content of 200 ppm or less; a chlorine content of 10 ppm or less; a boiling range of 500°F to 950°F (260°C to 510°C) or 500°F to 750°F (260°C to 399°C).

14. The process of claim 9, wherein the plastics feed comprises at least 10 wt. % polyethylene.

15. The process of claim 9, wherein the pyrolysis oil has a T99.5 cut point temperature in a range of from 480°C to 520°C.

16. The process of claim 9, wherein the combined feed comprises 1 to 49 wt. % of the pyrolysis oil relative to a combined weight of the pyrolysis oil and the waxy light neutral base oil.

17. The process of claim 9, wherein the combined feed comprises 10 to 30 wt. % of the pyrolysis oil relative to a combined weight of the pyrolysis oil and the waxy light neutral base oil.

18. The process of claim 9, further comprising recovering a Group 11+ 2 cSt base stock and a Group III 4 cSt base stock from the hydroisomerized effluent.

19. The process of claim 9, further comprising recovering a jet fuel from the hydroisomerized effluent.

20. A process for making a base stock, the process comprising:(a) providing a pyrolysis oil originating from the pyrolysis of a plastics feed comprising polyethylene, wherein the pyrolysis oil has a T99.5 cut point temperature in a range of from 480°C to 520°C;(b) providing a petroleum feedstock having a T5 to T95 boiling range of 316°C to 510°C;(c) combining the pyrolysis oil with the petroleum feedstock to form a combined feed, wherein the combined feed comprises 1 to 49 wt. % of pyrolysis oil relative to a combined weight of the pyrolysis oil and the petroleum feedstock;(d) hydrocracking the combined feed in a hydrocracking zone under hydrocracking conditions to produce a hydrocracked effluent;(e) separating the hydrocracked effluent into a gaseous fraction and a liquid fraction;(f) hydroisomerization dewaxing at least a portion of the liquid fraction in a hydroisomerization dewaxing zone under hydroisomerization dewaxing conditions to produce a hydroisomerized effluent;(g) recovering from the hydroisomerized effluent the base stock of claim 1.

21. The process of claim 20, wherein the pyrolysis oil is characterized by one or any combination of more than one of the following properties: an API gravity of 25 to 65; a wax content in the range of 30 to 90 wt. %; a nitrogen content of 500 ppm or less a sulfur content of 200 ppm or less; a chlorine content of 10 ppm or less; a boiling range of 500°F to 950°F (260°C to 510°C) or 500°F to 750°F (260°C to 399°C).

22. The process of claim 20, wherein the plastics feed comprises at least 10 wt. % polyethylene.

23. The process of claim 20, wherein the petroleum feedstock is characterized by one or any combination of more than one of the following properties: z / an API gravity in the range of 15 to 40; a viscosity index in the range of 30 to 90; a kinematic viscosity at 100°C in the range of 3 to 30 cSt; a wax content in the range of 5 to 20 wt. %; a nitrogen content of 1500 ppm or less a sulfur content of 4000 ppm or less.

24. The process of claim 20, wherein the petroleum feedstock comprises vacuum gas oil or is vacuum gas oil, or consists essentially of vacuum gas oil, or consists of vacuum gas oil.

25. The process of claim 20, wherein the vacuum gas oil is a light vacuum gas oil.

26. The process of claim 20, wherein the combined feed comprises 10 to 30 wt. % of the pyrolysis oil relative to a combined weight of the pyrolysis oil and the petroleum feedstock.

27. The process of claim 20, further comprising recovering a Group 11+ 2 cSt base stock and a Group III 4 cSt base stock from the hydroisomerized effluent.

28. The process of claim 20, further comprising recovering a jet fuel from the hydroisomerized effluent.

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