Continuous processes for converting plastic waste in recycling to normal alpha olefins and for the polymerization of polyethylene.

Abstract

CIRCULAR ECONOMY FOR PLASTIC WASTE TO POLYETHYLENE AND CHEMICALS VIA REFINERY CRUDE UNIT. A continuous process is provided to convert plastic waste in recycling for the polymerization of polyethylene or normal alpha olefins. The process comprises selecting plastic waste containing polyethylene and / or polypropylene and then passing the plastic waste through a pyrolysis reactor to thermally crack at least a portion of the olefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into excretion gas, a naphtha / diesel fraction, a heavy fraction, and charcoal. The naphtha / diesel fraction is passed to a crude unit in a refinery from which the direct-drive naphtha fraction (C5-C8) or the propane / butane fraction (C3-C4) is recovered. The direct-flow naphtha fraction, or the propane and butane (C3-C4) fraction, is passed to a steam cracker for the production of ethylene.Ethylene is converted in the normal alpha olefin and / or polyethylene synthesis unit. Also, a heavy fraction from the pyrolysis reactor can be combined with a heavy fraction of the normal alpha olefin stream recovered from the steam cracker. The combined heavy fraction and the heavy fraction of the normal alpha olefin stream can be passed to a wax hydrogenation zone to produce wax.

Description

1 / 30 “CONTINUOUS PROCESSES FOR CONVERTING PLASTIC WASTE INTO NORMAL ALPHA OLEFINS AND POLYETHYLENE POLYMERIZATION” FUNDAMENTALS

[0001] The world has witnessed extremely rapid growth in plastic production. According to PlasticsEurope Market Research Group, global plastic production was 335 million tons in 2016, 348 million tons in 2017, and 359 million tons in 2018. According to McKinsey & Company, the volume of global plastic waste was estimated at approximately 260 million tons per year in 2016 and projected to be 460 million tons per year in 2030 if the current trajectory continues.

[0002] Single-use plastic waste has become an increasingly important environmental problem. Currently, there appear to be few options for recycling polyethylene and polypropylene plastic waste into value-added chemicals and fuels. Currently, only a small amount of polyethylene and polypropylene is recycled via chemical recycling, where recycled and cleaned polymer granules are pyrolyzed in a pyrolysis unit to manufacture fuels (naphtha, diesel), flux cracker feed, or crude paraffin.

[0003] Processes are known that convert waste plastic into hydrocarbon lubricants. For example, U.S. Pat. No. 3,845,157 discloses the cracking of waste or virgin polyolefins to form gaseous products such as ethylene / olefin copolymers which are further processed to produce synthetic hydrocarbon lubricants. U.S. Pat. No. 4,642,401 discloses the production of liquid hydrocarbons by heating pulverized waste polyolefin at temperatures of 150 to 500°C and pressures of 2,000,000 to 3,000,000 Pascals (20 to 300 bar). U.S. Pat. No. 5,849,964 discloses a process in which waste plastic materials are depolymerized into a volatile phase and a liquid phase. The volatile phase is separated into a gaseous phase and a condensate. The liquid phase, condensate, and gas phase are refined into the following components: Petition 870260045608, dated 05 / 14 / 2026, page 8 / 77 2 / 30 liquid fuel using standard refining techniques. US Pat. No. 6,143,940 discloses a procedure for converting waste plastics into heavy wax compositions. US Pat. No. 6,150,577 discloses a process for converting waste plastics into lubricating oil. EP0620264 discloses a process for producing lubricating oil from waste or virgin polyolefins by thermally cracking the waste in a fluidized bed to form a waxy product, optionally using a hydrotreating, then catalytically isomerizing and fractionating to recover a lubricating oil.

[0004] Other documents relating to processes for converting plastic waste into lubricating oils include U.S. Patents Nos. 6,288,296, 6,774,272, 6,822,126, 7,834,226, 8,088,961, 8,404,912 and 8,696,994; and U.S. Patent Publication Nos. 2019 / 0161683; 2016 / 0362609; and 2016 / 0264885. The preceding Patent documents are incorporated herein by reference in their entirety.

[0005] The current method of chemical recycling via pyrolysis cannot cause a major impact on the plastics industry. Current pyrolysis operations produce fuel components of insufficient quality (products in the naphtha and diesel range), but the quantity is small enough that these products can be blended into fuel supplies. However, this simple blending cannot continue if very large volumes of residual polyethylene and polypropylene need to be recycled to address environmental problems. The products as produced from a pyrolysis unit are of too poor quality to be blended in large quantities (e.g., 5 to 20% by volume) into transportation fuels.

[0006] In order to achieve the recycling of single-use plastics in an industrially significant quantity to reduce their environmental impact, more robust processes are needed. Improved processes should establish a “circular economy” for polyethylene and polypropylene plastic waste where spent plastic waste is effectively recycled back as polymeric materials to high-value polymers and by-products. SUMMARY Petition 870260045608, dated 05 / 14 / 2026, page 9 / 77 3 / 30

[0007] A continuous process is provided for converting plastic waste into recycled material for polyethylene polymerization or normal alpha olefin synthesis. The process comprises first selecting plastic waste containing polyethylene and / or polypropylene. This plastic waste is then passed through a pyrolysis reactor to thermally crack at least a portion of the polyolefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into excretion gas, a naphtha / diesel fraction, a heavy fraction, and charcoal.

[0008] The incorporation of the process with an oil refinery is an important aspect of the present process and allows the creation of a circular economy with a single-use plastic waste such as polypropylene. Thus, the naphtha / diesel fraction is passed to a crude unit in a refinery, from which a direct-drive naphtha fraction is recovered. The direct-drive naphtha fraction is passed to a steam cracker for the production of ethylene.

[0009] The refinery will generally have its own hydrocarbon feed flowing through the refinery units. The volume of naphtha / diesel flow generated from the pyrolysis of plastic waste to the refinery units may comprise any practical or accommodative % volume of the refinery unit flow. Generally, the flow of the naphtha / diesel fraction generated from the pyrolysis of plastic waste, for practical reasons, may be up to about 50% by volume of the total flow, i.e., the refinery flow and the pyrolysis flow. In one embodiment, the pyrolysis flow of naphtha / diesel is an amount up to about 20% by volume of the total flow.

[0010] The pyrolyzed naphtha / diesel fraction is alternatively passed to a distillate treater, also known as a diesel hydrotreating unit, from which a light naphtha fraction (C5C8) is recovered. The light naphtha fraction is passed to a steam cracker for the production of ethylene.

[0011] Normal alpha olefins (NAO) are synthesized using ethylene recovered from the steam cracker and separated into several fractions, including a heavy (C22+) fraction of normal alpha olefins. This heavy fraction of normal alpha olefins is combined with the heavy fraction from the pyrolysis reactor. The heavy fraction Petition 870260045608, dated 05 / 14 / 2026, page 10 / 77 4 / 30 of the combined and heavy fraction of normal alpha olefin is then passed to a wax hydrogenation zone to produce wax.

[0012] In another embodiment, a continuous process for converting plastic waste in recycling for polyethylene polymerization is provided. The process comprises selecting plastic waste containing polyethylene and / or polypropylene and passing the plastic waste through a pyrolysis reactor to thermally crack at least a portion of the olefin waste and produce a pyrolyzed effluent. The pyrolyzed effluent is separated into expended gas, a naphtha / diesel fraction, a heavy fraction, and charcoal. The naphtha / diesel fraction is passed to a distillation column of the crude unit in a refinery from which a portion of the propane and butane (C3-C4) fraction is recovered from the distillation column. The C3-C4 fraction is then passed to a steam cracker for the production of ethylene.Ethylene is then passed to a normal alpha olefin (NAO) synthesis unit to produce valuable NAO chemicals in the C4 to C22+ range with recyclable content. A heavy fraction of normal alpha olefin (C22+) stream is recovered from the normal alpha olefin synthesis unit and combined with the heavy fraction from the pyrolysis reactor.

[0013] The combined heavy fraction and the normal alpha olefin stream heavy fraction are passed to a wax hydrogenation zone to produce hydrogenated wax (crude paraffin or paraffin wax).

[0014] Among other factors, it was found that through refinery addition operations, it can be found that pyrolysis oil from waste can be improved to higher value products such as gasoline and diesel. Also, through refinery addition operations, it was found that clean naphtha (C5-C8) or C3-C4 can be efficiently and effectively produced from pyrolysis oil from waste for the final production of polyethylene polymer. Positive economies are achieved for the overall process from recycled plastics to a polypropylene product with product quality identical to that of virgin polymer. BRIEF DESCRIPTION OF THE DRAWINGS

[0015] FIG 1 represents the current practice of pyrolyzing plastic waste to Petition 870260045608, dated 05 / 14 / 2026, page 11 / 77 5 / 30 produce fuel or wax (base case).

[0016] FIG. 2 represents a present process for establishing a circular economy for plastic waste.

[0017] FIG. 3 represents the classification of plastic type for recycling plastic waste. DETAILED DESCRIPTION

[0018] In the present process, a method is provided for recycling waste polyethylene and polypropylene back into virgin polyethylene to establish a circular economy by combining three distinct industrial processes. A substantial portion of polyethylene and polypropylene polymers are used in single-use plastics and discarded after their use. Single-use plastic waste has become an increasingly important environmental problem. Currently, there appear to be few options for recycling polyethylene and polypropylene plastic waste into value-added chemicals and fuel products. Currently, only a small amount of polyethylene / polypropylene is recycled via chemical recycling, where recycled and clean polymer granules are pyrolyzed in a pyrolysis unit to manufacture fuels (naphtha, diesel), steam cracker feed, or paraffin.

[0019] Ethylene is the most widely produced petrochemical building block. Ethylene is produced in hundreds of millions of tons per year via steam cracking. Steam crackers use gaseous feedstocks (ethane, propane and / or butane) or liquid feedstocks (naphtha or gas oil). It is a non-catalytic cracking process operating at very high temperatures, up to 850°C.

[0020] Polyethylene is widely used in various consumer and industrial products. Polyethylene is the most common plastic, but 100 million tons of polyethylene resins are produced annually. Its primary use is in packaging (plastic bags, plastic films, geomembranes, containers including bottles, etc.). Polyethylene is produced in three main forms: high-density polyethylene (HDPE, ~0.940 to 0.965 g / cm-3), linear low-density polyethylene Petition 870260045608, dated 05 / 14 / 2026, page 12 / 77 6 / 30 (LLDPE, ~0.915 to 0.940 g / cm-3) and low-density polyethylene (LDPE, (< 0.930 g / cm-3), with the same chemical formula (C2H4)n but different molecular structure. HDPE has a low degree of branching with short side chains while LDPE has a very high degree of branching with long side chains. LLDPE is a substantially linear polymer with significant numbers of short branches, usually made by copolymerization of ethylene with short-chain alpha-olefins.

[0021] Low-density polyethylene (LDPE) is produced via radical polymerization at 150 to 300°C and very high pressure of 1,000 to 3,000 atm. The process uses a small amount of oxygen and / or organic peroxide initiator to produce a polymer with about 4,000 to 40,000 carbon atoms per average polymer molecule. and with many ramifications.High-density polyethylene (HDPE) is manufactured at relatively low pressure (10 to 80 atm) and 80 to 150°C in the presence of a catalyst. Organometallic Ziegler-Natta catalysts (titanium(III) chloride with an aluminum alkyl) and Phillips-type catalysts (chromium(IV) oxide in silica) are typically used, and manufacturing is done via a fluidized paste process using a loop reactor or via a gas-phase process with a fluidized bed reactor. Hydrogen is mixed with ethylene to control the polymer chain length. The manufacturing conditions for linear low-density polyethylene (LLDPE) are similar to those of HDPE except for the copolymerization of ethylene with short-chain alpha-olefins (1-butene or 1-hexene).

[0022] Currently, only a small portion of spent polyethylene products is collected for recycling, due to the inefficiencies and ineffectiveness of recycling efforts discussed above.

[0023] FIG. 1 shows a diagram of the pyrolysis of fuel or wax from waste plastic that is commonly operated in industry today. As mentioned above, generally, polyethylene and polypropylene waste are sorted together 1. Clean polyethylene / polypropylene waste 2 is converted in a pyrolysis unit 3 to release gas 4 and pyrolysis oil (liquid product). The release gas 4 from the pyrolysis unit is used as fuel to operate the pyrolysis unit 3, and only the pyrolysis unit is used for commercial purposes. A Petition 870260045608, dated 05 / 14 / 2026, page 13 / 77 7 / 30 Local distillation unit separates pyrolysis oil to produce naphtha and diesel products 5 which are sold to fuel markets. The heavy oil fraction from pyrolysis 6 is recycled back to pyrolysis unit 3 to maximize fuel yield. Charcoal 7 is removed from pyrolysis unit 3. The heavy fraction 6 is rich in long-chain, linear hydrocarbons and is very waxy (i.e., forms paraffin wax upon cooling to room temperature). The wax can be separated from the heavy fraction 6 and sold to wax markets.

[0024] The present process converts pyrolyzed polyethylene and / or polypropylene plastic waste in large quantities by integrating the product streams from the pyrolysis of residual polymer into an oil refinery operation. The resulting processes produce feedstocks for the polymers (naphtha or C3-C4 for ethylene cracker), as well as high-quality gasoline and diesel fuel and / or high-quality base oil.

[0025] Generally, the present process provides a circular economy for polyethylene plants. Polyethylene is produced via polymerization of pure ethylene. Clean ethylene can be manufactured using a steam cracker. Naphtha or a C3-C4 stream can be fed to the cracker with steam. The ethylene is then polymerized to create polyethylene.

[0026] Through refinery operations to improve the pyrolysis of waste oil to higher value products (gasoline, jet and diesel) and to produce clean LPG and naphtha for steam crackers for the final production of polyethylene polymer, a person is able to create positive economies for the overall process from recycled plastics to ethylene product with product quality identical to that of virgin polymer.

[0027] A pyrolysis unit produces products of insufficient quality containing contaminants such as calcium, magnesium, chlorides, nitrogen, sulfur, dienes, and heavy components, which cannot be used in larger quantities to blend into transportation fuels. It has been found that as these products pass through the refinery units, the contaminants can be captured in the pre-treatment units, causing negative impacts. Petition 870260045608, dated 05 / 14 / 2026, page 14 / 77 8 / 30 reduced. Fuel components can be further enhanced with appropriate refinery units with chemical conversion processes, with the final transport fuels produced by the integrated process being of superior quality and meeting fuel quality requirements. The integrated process will generate a much cleaner naphtha stream as feedstock for steam cracker generation and polyethylene production. These large productions within specifications allow for a practicable “cycle economy” for plastics recycling.

[0028] Carbon in and out of refinery operations is “transparent,” meaning that not all molecules of plastic waste necessarily end up in the exact olefin product cycled back to the polyolefin plants, but are nevertheless taken as “credit” as the net “green” carbon in and out of the refinery is positive. With these integrated processes, the amount of virgin feedstock needed for polyethylene plants will be substantially reduced.

[0029] FIG. 2 shows the present integrated process, integrating refinery operations with recycling for the production of efficient polyethylene. In FIG. 2, mixed plastic waste is sorted together 21. The clean plastic waste 22 is converted in a pyrolysis unit 23 to expulsion gas 24 and a pyrolysis oil (liquid product) and optionally wax (solid product at room temperature). The expulsion gas 24 from the pyrolysis unit can be used as fuel to operate the pyrolysis unit 23. The pyrolysis oil is separated, usually in an on-site distillation unit, into a naphtha / diesel fraction 25 and a heavy fraction 26. The charcoal 27 is removed from the pyrolysis unit 23 after completion of the pyrolysis step.

[0030] The pyrolysis unit may be located near the plastic waste collection site, which may be far from, near, or inside a refinery. If the pyrolysis unit is located far from the refinery, then the pyrolysis oil (naphtha / diesel and heavy fuel oil) can be transferred to the refinery by truck, barge, railcar, or pipeline. However, it is preferred that Petition 870260045608, dated 05 / 14 / 2026, page 15 / 77 9 / 30 that the pyrolysis unit is located within the plastics collection site or refinery.

[0031] The preferred starting material for the present process is graded plastic waste containing predominantly polyethylene and polypropylene (plastic recycling classification types 2, 4 and 5). The pre-graded plastic waste is washed and shredded or granulated for feeding into a pyrolysis unit for thermal cracking. FIG. 3 represents the plastic type classification for plastic waste recycling. Classification types 2, 4 and 5 are high-density polyethylene, low-density polyethylene and low-density polypropylene, respectively. Any combination of polyethylene and polypropylene plastic waste can be used. For the present process, at least some polyethylene plastic waste is preferred.

[0032] Proper sorting of plastic waste is very important in order to minimize contaminants such as N, Cl and S. Plastic waste containing polyethylene terephthalate (plastic recycling classification type 1), polyvinyl chloride (plastic recycling classification type 3) and other polymers (plastic recycling classification type 7) must be sorted to less than 5%, preferably less than 1% and most preferably less than 0.1%. The present process can tolerate a moderate amount of polystyrene (plastic recycling classification type 6). Residual polystyrene must be sorted to less than 30%, preferably less than 20% and most preferably less than 5%.

[0033] Washing plastic waste removes metallic contaminants such as sodium, calcium, magnesium, and aluminum, and non-metallic contaminants originating from other waste sources. Non-metallic contaminants include contaminants originating from Group IV of the Periodic Table, such as silica; Group V contaminants, such as phosphorus and nitrogen compounds; Group VI contaminants, such as sulfur compounds; and Group VII halide contaminants, such as fluoride, chloride, and iodide. Residual metals, non-metallic contaminants, and halides need to be removed to less than 50 ppm, preferably less than 30 ppm, and most preferably to Petition 870260045608, dated 05 / 14 / 2026, page 16 / 77 10 / 30 less than 5 ppm.

[0034] If washing does not remove metals, non-metallic contaminants and halide impurities adequately, then a separate protective bed may be used to remove metals and non-metallic contaminants.

[0035] Pyrolysis is carried out by contacting a feedstock of plastic material in a pyrolysis zone under pyrolysis conditions, where at least a portion of the feed(s) is cracked, thereby forming a pyrolysis zone effluent comprising olefins and paraffins. Pyrolysis conditions include a temperature of about 400°C to about 700°C, preferably about 450°C to about 650°C. Conventional pyrolysis technology employs operating conditions of pressures above atmospheric. See, for example, US Pat. No. 4,642,401. Additionally, it has been found that by adjusting the pressures downwards, the yield of a desired product can be controlled. See, for example, US Pat. No. 6,150,577. Consequently, in some embodiments where such control is desired, the pyrolysis pressure is subatmospheric.

[0036] FIG. 2 shows the present integrated process where only the naphtha / diesel fraction 25 from the pyrolysis unit is sent to the crude unit's desalter 28 to produce C5-C8 naphtha stream, preferably C5-C7 naphtha and most preferably C5-C6 naphtha 29 which is used to feed the cracker with steam to generate ethylene. The ethylene is passed to a polymerization unit 40, with the polyethylene polymer product used for polyethylene consumer products 41. The heavy naphtha / diesel / gas oil 30 are sent to the appropriate refinery units 31 for upgrading into clean gasoline, diesel or jet fuel.

[0037] The crude refinery unit separates crude oil into multiple fractions such as liquefied petroleum gas (LPG), naphtha, kerosene, diesel, and gas oil, which will be further processed into useful petroleum products. The crude refinery unit has a crude treatment section, commonly known as a desalter, and a crude oil distillation or fractionation section. The distillation section typically includes an atmospheric distillation unit and a unit of Petition 870260045608, dated 05 / 14 / 2026, page 17 / 77 11 / 30 vacuum distillation.

[0038] The naphtha / diesel fraction from the pyrolysis unit is fed to the desalter which removes salts and solids contained in the oil to protect downstream equipment from the harmful effects of contaminants. To remove the salts, water is mixed with the oil and typically heated to temperatures between about 102°C (215°F) and about 138°C (280°F) and allowed to separate in the desalting unit.

[0039] The refinery will generally have its own hydrocarbon feed flowing through the refinery units. The volume of naphtha / diesel flow generated from the pyrolysis of plastic waste to the refinery units, for example, the crude refinery unit in the present process, may comprise any % of the total flow volume, whether practical or accommodative, to the refinery units. Generally, the flow of the naphtha / diesel fraction generated from the pyrolysis of plastic waste, for practical reasons, may be up to about 50% by vol. of the total flow, i.e., of the refinery flow and the pyrolysis flow. In one embodiment, the naphtha / diesel flow from pyrolysis is an amount up to about 20% by vol. of the total flow. In another embodiment, the naphtha / diesel flow from pyrolysis is an amount up to about 10% by vol. of the total flow. About 20% by vol.The amounts determined were quite practical in their impact on the refinery, while also providing excellent results and being manageable. The amount of naphtha / diesel generated from pyrolysis can naturally be controlled so that the fraction passed to the refinery units provides the desired volume percentage of the flow.

[0040] Desalted oil is sent to an atmospheric distillation unit heated to approximately 340 to 372°C (644 to 700°F) at the bottom of the distillation column, and the liquid is removed at various points along the fractional distillation column to produce various fuels. Fuels from the crude units can be sent to various enhancement units in the refinery to remove impurities (nitrogen, sulfur) and to catalytically transform the fractions to improve product properties such as octane and cetane numbers. The residue of Petition 870260045608, dated 05 / 14 / 2026, page 18 / 77 12 / 30 of the bottom of the atmospheric distillation column, also known as atmospheric residue, is sent to a vacuum distillation column to produce vacuum gas oil (343 to 566°C (650 to 1050°F)) and vacuum residue. The vacuum gas oil can be used to produce base oil or further cracked to produce gasoline, jet fuel, and diesel. The overall process produces LPG (<27°C (<80°F)), gasoline (27 to 204°C (80-400°F)), jet fuel (182 to 260°C (360-500°F)), and diesel (149 to 371°C (300-700°F)). The boiling points for these fractions are adjusted depending on the season and local specifications.

[0041] Alternatively, the naphtha / diesel fraction is passed to a distillate hydrotreator, also known as a diesel hydrotreator, for mild hydrotreating. The hydrotreating step saturates portions of olefins, dienes, and aromatics to improve fuel quality. Typical hydrotreating conditions used to remove contaminants while preventing cracking include temperatures ranging from about 190°C (374°F) to about 340°C (644°F), pressures ranging from about 2700 kPa (400 psig) to about 20700 kPa (3000 psig), space velocities (LHSV) in the range of about 0.1 h-1 to about 20 h-1, and hydrogen recycle rates ranging from about 400 to about 15,000 SCF / B. Hydrotreating catalysts include those conventionally used in hydrotreating units, containing metals such as Ni, Mo, Co, W and porous supports such as alumina, silica, silica-alumina.A fraction of light naphtha (C5-C8) can be recovered from the hydrotreator and then passed to a steam cracker for the production of ethylene.

[0042] Normal alpha olefins are synthesized in the normal alpha olefin synthesis unit at 36 using ethylene recovered from the steam cracker 35. Several fractions of normal alpha olefins are recovered. The manufacturing process in the normal alpha olefin synthesis unit converts ethylene to linear alpha olefins via ethylene oligomerization. There are several commercial processes that oligomerize ethylene to linear alpha olefins with a wide distribution of carbon numbers in the range C4 to C30. The most common Ziegler process uses triethyl aluminum as a catalyst and excess ethylene is fed to a buffered flow reactor. A Petition 870260045608, dated 05 / 14 / 2026, page 19 / 77 13 / 30 The reaction is conducted at high pressure and high temperature. Excess ethylene is vaporized. The triethyl aluminum catalyst is washed from the product with caustic soda, and the linear alpha olefins are separated.

[0043] The heavy, serous fraction 26 of the pyrolysis oil from the pyrolysis unit is combined with a unit product stream from the normal alpha olefin (NAO) synthesis unit of heavy C22+ NAO 37 recovered from the NAO synthesis unit 36. Then the combined heavy NAO stream is hydrotreated 38 to produce wax, crude paraffin or paraffin wax.

[0044] The ethylene polymerization unit is preferably located close to the refinery so that the feedstock (propane, butane, naphtha) can be transferred via pipeline. For the petrochemical plant located far from the refinery, the feedstock can be delivered via truck, barge, railcar or pipeline.

[0045] In another embodiment, the C3-C4 fraction 32 is recovered from the refinery crude unit 28. This stream can also be fed to the steam cracker 35 for the production of ethylene. The ethylene is passed through a polymerization unit 40, with the polyethylene product used for consumer polyethylene products 41.

[0046] The benefits of a circular economy and an effective and efficient recycling campaign are realized by this integrated process.

[0047] The following examples are provided to further illustrate the present process and its benefits. The examples are intended to be illustrative and not limiting. Example 1: Properties of Pyrolysis Oil and Wax from Commercial Sources

[0048] The pyrolysis oil and wax samples were obtained from commercial sources and their properties are summarized in Table 1. These pyrolysis samples were prepared from plastic waste containing mostly polyethylene and polypropylene via thermal decomposition in a pyrolysis reactor at around 400 to 600°C, near atmospheric pressure without any added gas or catalyst. A pyrolysis unit typically produces gas, liquid oil product, Petition 870260045608, dated 05 / 14 / 2026, page 20 / 77 14 / 30 optionally wax and charcoal product. The top gas stream from the pyrolysis unit containing thermally cracked hydrocarbon has been cooled to collect condensate as pyrolysis oil (liquid at room temperature) and / or pyrolysis wax (solid at room temperature). Pyrolysis oil is the main product of pyrolysis units. Some units produce pyrolysis wax as a separate product in addition to pyrolysis oil. Table 1

[0049] Properties of Oil and Wax as Received from the Pyrolysis of Plastic Waste Pyrolysis Oil Sample A Pyrolysis Oil Sample B Pyrolysis Oil Sample C Pyrolysis Oil Sample D Pyrolysis Wax Sample E Specific Gravity at 16°C 0.814 0.820 0.774 -0.828 (60°F) Simulated Distillation, °C (°F) 30 (87) 148 (299) -8 (18) 30 (86) 163 (325) 0.5% (Initial Boiling Point) 82 (179) 152 (306) 54 (129) 68 (154) 246 (475) 101 (214) 154 (309) 69 (156) 99 (210) 285 (545) 5% 161 (322) 174 (346) 140 (285) 151 (304) 347 (656) 10% 216 (421) 230 (447) 200 (392) 216 (421) 389 (733) 30% 285 (545) 307 (585) 269 (517) 278 (532) 426 (798) 50% 369 (696) 426 (798) 350 (663) 358 (676) 479 (894) 70% 411 (772) 473 (883) 390 (735) 395 (743) 504 (939) 90% 506 (942) 582 510 (951) 476 (888) 573 (1064) 95% (1079) 99.5% (Final Boiling Point) Carlo-Erba Hydrocarbon Analysis Petition 870260045608, dated 05 / 14 / 2026, page 21 / 77 15 / 30 Carbon, % by weight 87.6 84.21 85.46 85.97 85.94 Hydrogen, % by weight 12.7 12.25 14.1 14.0 14.15 Sum of C + H, % by weight 100.3 96.46 99.5 100.0 100.1 1.73 1.75 1.98 1.96 1.98 Molar Ratio H / C Bromine Number, g / 100 49 60 40 44 14 g Hydrocarbon Type Total Aromatics, vol% 23.3 22.8 5.1 8.7 13.3 Total Olefins & 39.0 50.2 42.4 38.2 42.1 Naphthenes, % Total Paraffins, % by volume 37.7 27 52.5 53.1 44.6 Contaminants Total Sulfur, ppm 48 29 7.8 99 6.3 Total Nitrogen, ppm 751 1410 318 353 237 Total Cl, ppm 113 62 41 70 4.7 Oxygen in naphtha & distillate, 250 - 574 - - ppm Trace Element Impurities <1.1 <0.56 0.6 <0.53 <0.68 Al, ppm 1.4 11.5 <0.5 <0.53 <0.68 Ca, ppm 4.9 11.9 1.6 <1.1 3.1 Fe, ppm <0.51 1.3 <0.52 <0.53 <0.68 Mg, ppm 2.5 <0.54 <1.1 <2.2 <2.7 Na, ppm <0.51 <0.54 <0.52 2 <0.68 Ni, ppm <0.51 <0.54 <0.52 4 <0.68 V, ppm 8.2 9.9 <1.6 <2.2 20.2 P, ppm 82.5 49.6 13 17 3.1 Si, ppm Petition 870260045608, dated 05 / 14 / 2026, page 22 / 77 16 / 30

[0050] The ASTM D4052 method was used for specific gravity measurements. The simulated boiling point distribution curve was obtained using the ASTM D2887 method. Carlo-Erba analysis for carbon and hydrogen was based on the ASTM D5291 method. Bromine number measurement was based on the ASTM D1159 method. Hydrocarbon type analysis was performed using a high-resolution magnetic mass spectrometer using a scanned magnet from 40 to 500 Daltons. Total sulfur was determined using the XRF method according to ASTM D2622. Nitrogen was determined using a modified ASTM D5762 method using chemiluminescence detection. Total chloride content was measured using a combustion ion chromatography instrument using the modified ASTM 7359 method. The nitrogen content in naphtha and the boiling range of the distillate were estimated using GC by GC / MS measurements with an electron ionization detector for the m / Z range of 29 to 500.Metallic and non-metallic trace elements in oil were determined using inductively coupled plasma atomic emission spectrometry (ICP-AES).

[0051] The industrial pyrolysis process of graded plastics, originating predominantly from polyethylene and polypropylene waste, produced hydrocarbon streams of quality with specific gravity ranging from 0.7 to 0.9 and a boiling range of -8 to 593°C (18 to 1100°F) as in pyrolysis oil or pyrolysis wax.

[0052] The pyrolysis product is a fairly pure hydrocarbon composed mostly of carbon and hydrogen. The hydrogen-to-carbon molar ratio varies from 1.7 to almost 2.0. The bromine number ranges from 14 to 60, indicating varying degrees of unsaturation originating from olefins and aromatics. The aromatic content ranges from 5 to 23% by volume, with a higher severity unit producing more aromatics. Depending on the process conditions of the pyrolysis unit, the pyrolysis products exhibit paraffinic content ranging from mid-20% by vol. to mid-50% by vol. The pyrolysis product contains a substantial amount of olefins. Samples A and B are pyrolysis oil produced under more severe conditions such as higher pyrolysis temperature and / or residence time. Petition 870260045608, dated 05 / 14 / 2026, page 23 / 77 Samples 17 / 30, which are longer, contain higher aromatic and lower paraffinic components, resulting in an H / C molar ratio around 1.7 and a higher Bromine Number of 50 to 60. Samples C and D were produced under less harsh conditions, and the pyrolysis oils are more paraffinic, resulting in an H / C molar ratio close to 2.0 and a Bromine Number around 40. Sample E, pyrolysis wax, is mostly paraffinic hydrocarbon, saturated with a substantial amount of normal hydrocarbons (as opposed to branched hydrocarbons) with a low Bromine Number of only 14.

[0053] The following Examples 2 to 5 present the evaluation of pyrolysis oil from waste plastic for transport fuel. Example 2: Fractionation of Pyrolysis Oil for Evaluation as a Transportation Fuel

[0054] Sample D was distilled to produce hydrocarbon cuts representing gasoline (177°C (350°F-)), jet fuel (177 to 300°C (350 to 572°F)), diesel (300 to 371°C (572 to 700°F)) and the heavy fractions (371°C (700°F+)). Table 2 summarizes the boiling point distribution and impurity distributions among the distillate product fractions. Table 2

[0055] Pyrolysis Oil Distillation into Fuel Fractions Petition 870260045608, dated 05 / 14 / 2026, page 24 / 77 18 / 30 Sample ID Sample D Sample F Sample G Sample H Sample 1 Intended Fraction Gasoline Cut Jet Cut Diesel Cut Unconverted Cut Point Target, °F 350' 350-572 572-700 700+ Distillation Actual Yields, wt% 37.2 38.0 15.0 9.3 Simulated Distillation, F IBP(0.5wt%) 86 27 299 539 640 5 wt% 154 98 345 557 684 10 wt% 210 147 365 574 696 30 wt% 304 222 416 597 727 50 wt% 421 270 457 619 758 70 wt%532 291 492 644 808 90 wt% 676 337 546 674 898 95 wt% 743 347 554 683 953 FBP (99.5 wt%) 888 385 591 711 1140 Total S, ppm 99 52 35 80 320 Total N, ppm 353 215 556 232 467 Total Cl, ppm 70 181 27 12 13 Example 3: Evaluation of Pyrolysis Oil Cut-Off for Fuel Gasoline

[0056] Sample F, a pyrolysis oil cut for the boiling range of gasoline fuel, was evaluated to estimate its potential for use as gasoline fuel. Sample F has the carbon number range of C5 to C12, typical of gasoline fuel.

[0057] Due to the olefinic nature of pyrolysis oil, oxidation stability (ASTM D525) and gum-forming tendency (ASTM D381) were identified as the most critical properties to examine. Theoretical octane rating (RON) and engine octane rating (MON) are also critical properties for engine performance. RON and MON values ​​were estimated from detailed hydrocarbon GC analysis. Table 3

[0058] Evaluation of the Naphtha Fraction of Pyrolysis Oil for Fuel Gasoline Washed Gum Stability, RON MON Petition 870260045608, dated 05 / 14 / 2026, page 25 / 77 19 / 30 Oxidation, min mg / 100 mL Sample F 90 5.0 71.4 67.7 Reference gasoline >1440 1 95.8 30 (86).2 4 / 96 % by vol. of Combination of Sample F with reference gasoline >1440 2.0 94.5 85.1 15 / 85 % by vol. of Combination of Sample F with reference gasoline >1440 2.2 91.8 83.1

[0059] Sample F, a pyrolysis oil cutoff for the boiling range of fuel gasoline, cannot be used on its own as automotive fuel gasoline due to its insufficient quality. The gasoline fraction of the pyrolysis oil showed very insufficient oxidation stability, with Sample F failing only after 90 min compared to the target stability of no longer than 1440 minutes. The pyrolysis gasoline exceeded the target washing gum of 4 mg / 100 mL, suggesting a severe tendency for gum formation. The pyrolysis gasoline has insufficient octane numbers compared to the reference gasoline. A premium unleaded gasoline was used as the reference gasoline.

[0060] We also examined the potential for combining pyrolysis gasoline cut to a limited quantity relative to reference gasoline. Our study showed that possibly up to 15% by volume of Sample F can be combined with refinery gasoline while still meeting the appropriate fuel targets. By integrating the pyrolysis gasoline product with a refinery fuel, the overall product quality can be maintained.

[0061] These results indicate that the fraction of gasoline as produced from pyrolysis oil has limited utility as gasoline fuel. Improvement in a refinery unit is preferred to convert this gasoline fraction from the oil. Petition 870260045608, dated 05 / 14 / 2026, page 26 / 77 20 / 30 pyrolysis in hydrocarbon that achieves the target properties of gasoline fuel. Example 4: Evaluation of Pyrolysis Oil Cut-Off for Jet Fuel

[0062] Sample G, a pyrolysis oil cut for the boiling range of jet fuel, was evaluated to estimate its potential for use as jet fuel. Sample G has a carbon number range of C9 to C18, typical of jet fuel.

[0063] Due to the olefinic nature of pyrolysis oil, the thermal oxidation test of jet fuel (D3241) was considered the most critical test. The jet cut of pyrolysis oil as such, sample G, had only 36 minutes of oxidation stability, suggesting that the pyrolysis cut for pure jet is unsuitable for use as jet fuel.

[0064] We prepared a 5% by volume combination of pyrolysis jet fuel (Sample G) with jet fuel produced at the refinery. The combination still failed the jet fuel oxidation test as shown in Table 4. Table 4

[0065] Evaluation of the Jet Fraction of Pyrolysis Oil for Jet Fuel Thermal Oxidation Test of Jet Fuel Reference jet fuel Passed 5 / 95% by volume of the combination of Sample G with reference jet fuel Failed

[0066] These results indicate that the jet fraction as produced from pyrolysis oil is completely unsuitable for jet fuel and an improvement in a refinery unit is required to convert this jet fraction from pyrolysis oil into hydrocarbon that achieves the target jet fuel properties. Petition 870260045608, dated 05 / 14 / 2026, page 27 / 77 21 / 30 Example 5: Evaluation of Pyrolysis Oil Cut-Off for Diesel Fuel

[0067] Sample H, a pyrolysis oil cutoff for the boiling range of diesel fuel, was evaluated to estimate its potential for use as diesel fuel. Sample H has the carbon number range of C14 to C24, typical of diesel fuel.

[0068] Sample H contains a substantial amount of normal hydrocarbons. Since normal hydrocarbons tend to exhibit waxy characteristics, cold flow properties such as pour point (ASTM D595014) and cloud point (ASTM D5773) were considered the most critical tests.

[0069] We prepared two combinations at 10 and 20% by volume of Sample H with refinery-produced diesel fuel. However, both combinations still failed to meet the target spill point of less than -17.8°C (0°F). Table 5

[0070] Evaluation of the Diesel Fraction of Pyrolysis Oil for Diesel Fuel Cloud Point (°C) Pour Point (°C) Pour Point Test Reference Diesel Fuel -17.1 -19.0 Passed Combination of 10 / 90% by volume of Sample H with reference diesel fuel -11.1 -12.0 Failed Combination of 20 / 80% by volume of Sample H with reference diesel fuel -5.5 -7.0 Failed

[0071] These results indicate that pyrolysis oil as such is completely Petition 870260045608, dated 05 / 14 / 2026, page 28 / 77 22 / 30 is unsuitable for diesel fuel, and improvements to a refinery unit are required to convert the diesel fraction of the pyrolysis oil into a hydrocarbon that meets the target properties of diesel fuel. Example 6: Co-processing of Pyrolysis Oil for the Crude Oil Unit or Desalination Unit

[0072] The results in Table 1 showed that the industrial pyrolysis process of graded plastics, originating predominantly from polyethylene and polypropylene waste, produced pyrolysis oil or pyrolysis wax of good quality composed mostly of carbon and hydrogen. With good grading and efficient pyrolysis unit operation, nitrogen and sulfur impurities are at sufficiently low levels that a modern refinery can handle feeding pyrolysis feedstocks to its processing units without any detrimental impact.

[0073] However, some pyrolysis oils or waxes may still contain high amounts of metals (Ca, Fe, Mg) and other non-metals (P, Si, Cl, O) that would negatively affect the performance of conversion units in a refinery. Pyrolysis products with high impurity levels are preferably fed to a desalting unit before the raw unit so that the bulk of the impurities are effectively removed by the desalter.

[0074] By feeding the pyrolysis feedstock to a crude unit or to a desalting unit prior to the crude unit, the pyrolysis oil will be fractionated into multiple components and then converted in subsequent conversion units including paraffin isomerization unit, jet hydrotreating unit, diesel hydrotreating unit, fluid catalytic cracking (FCC) unit, alkylation unit, hydrocracking unit and / or coking unit to manufacture gasoline, jet fuel and diesel with satisfactory product properties. The conversion units (FCC or hydrocracking unit) will also convert the heavy cut (corresponding to Sample I) into quality transportation fuels. After the crude unit, the pyrolysis oil will be further converted in the units of Petition 870260045608, dated 05 / 14 / 2026, page 29 / 77 23 / 30 subsequent conversions. The following Example 7 demonstrates the conversion of pyrolysis oil from waste plastics into quality transportation fuel in a refinery conversion unit, using an FCC unit as an example. Example 7: Conversion of Pyrolysis Oil to FCC

[0075] To study the impact of co-processing pyrolysis oil from waste plastic for FCC, a series of laboratory tests were carried out with Samples A and C. Vacuum gas oil (VGO) is the typical feed for FCC. The FCC performances of combining 20% ​​pyrolysis oil with VGO and pure pyrolysis oil were compared with those of pure VGO feed.

[0076] FCC experiments were performed in a Model C ACE (Advanced Cracking Evaluation) unit manufactured by Kayser Technology Inc. using regenerated equilibrium catalyst (Ecat) from a refinery. The reactor was a fixed fluidized reactor using N2 as the fluidizing gas. Catalytic cracking experiments were performed at atmospheric pressure and a reactor temperature of 482°C (900°F). The cat / oil ratio was varied between 5 and 8 by varying the amount of catalyst. A gaseous product was collected and analyzed using a refinery gas analyzer (RGA) equipped with a GC with a FID detector. In situ regeneration of spent catalyst was performed in the presence of air at 704°C (1300°F), and the regenerated fuel gas was passed through a LECO unit to determine the coke yield. A liquid product was weighed and analyzed in a GC for simulated distillation (D2830 (87)) and analysis of the C5 composition.With a material balance, the yields of coke, dry gas components, LPG components, gasoline (C5-221°C (430°F)), light cycle oil (LCO, 221°C to 343°C (430 to 650°F)) and heavy cycle oil (HCO, 343°C+(650°F+)) were determined. The results are summarized below in Table 6. Table 6

[0077] Evaluation of Pyrolysis Oil Co-feeding for FCC 100% VGO Feeding Mixture of 20 / 80% by volume, 20 / 80% by volume Mixture, 100% Sample A, 100% Sample C Petition 870260045608, dated 05 / 14 / 2026, page 30 / 77 24 / 30 Sample A / VGO Sample C / VGO Cat / Oil, w / w 6.0 6.0 6.0 6.0 6.0 Conversion, % 81.3 83.15 83.09 76.1 78.82 by weight* WLP Impurity** 81 76 62 54 67 Total O2, ppm 27 30 33 50 21 Total N2, ppm Coke Yield, % by weight 4.45 4.35 4.20 3.56 2.90 Total Dry Gas, 2.08 1.96 1.93 1.55 1.43 % by weight 0.16 0.12 0.12 0.05 0.04 Hydrogen 0.68 0.65 0.64 0.50 0.46 Methane 0.44 0.43 0.41 0.33 0.28 Ethane 0.76 0.74 0.72 0.63 0.61 Ethylene LPG Total, % 21.25 21.08 21.50 20.17 24.40 by weight 1.78 1.76 1.72 1.47 1.53 Propane 5.53 5.51 5.56 5.57 6.75 Propylene 1.56 1.56 1.54 1.29 1.34 n-Butane 6.61 6.48 6.64 5.43 6.61 Isobutane 5.77 5.77 6.04 6.41 8.16 C4 Olefins Gasoline, % in 53.53 55.75 55.46 62.53 61.75 weight 12.89 12.23 11.93 10.37 8.03 LCO, % in 5.81 4.63 4.98 1.82 1.50 weight HCO, % in Petition 870260045608, dated 05 / 14 / 2026, page 31 / 77 25 / 30 weight Octane Index*** 88.05 84.57 82.79 73.75 75.41

[0078] *: Conversion - conversion of the fraction 221 °C+ to 221°C-(430oF+ to 430oF-)

[0079] **: Level of N and O impurities in the whole liquid product in the boiling range of fuels by GC x GC, ppm

[0080] ***: Octane number, (R+M) / 2, was estimated from the detailed FCC gasoline hydrocarbon GC.

[0081] The results in Table 6 show that up to 20% by volume of pyrolysis oil co-feed only makes the changes in FCC unit performance very slight, indicating that pyrolysis oil co-processing up to 20% is easily practicable. The 20% by volume combination of Sample A or Sample C led to a very slight reduction in coke and dry gas yields, a slight increase in gasoline yield, and a slight decrease in LCO and HCO, which are favorable in most situations. With the paraffinic nature of pyrolysis oil, the 20% combinations of A and C decreased the Octane Index by about 3 to 5 numbers. With refinery operational flexibility, these Octane Index losses can be compensated for with local adjustments to the combination or feed.

[0082] By co-feeding pyrolysis oil through the FCC process unit with a zeolite catalyst, oxygen and nitrogen impurities in the fuel range were substantially reduced, from about 300 to 1400 ppm N to about 30 ppm N and from about 250 to 540 ppm O to about 60 to 80 ppm O. The hydrocarbon composition of all these co-feed products is well within the typical FCC gasoline range.

[0083] FCC rounds of 100% pyrolysis oil showed substantial Octane Number drops of around 13 to 14. This shows that co-processing pyrolysis oil is preferable to processing 100% pure pyrolysis oil. Example 8: C3-C4 and / or Naphtha Generation Feedstocks via Product of Petition 870260045608, dated 05 / 14 / 2026, page 32 / 77 26 / 30 Pyrolysis of Plastic Waste Feeding to Refinery Crude Unit

[0084] By feeding whole pyrolysis oil to a crude unit or to a desalting unit before the crude unit, the pyrolysis oil will be fractionated into multiple components. With pyrolysis oil feed, the refinery crude unit produces substantial quantities of clean propane, butane and naphtha streams, as well as other streams for refinery conversion units. Example 9: Feeding C3-C4 and / or Naphtha Recycling to the Steam Cracker for Ethylene Production, Followed by the Production of Circular Polyethylene Resin and Polyethylene Consumer Products

[0085] The propane, butane, and naphtha streams produced via co-feeding pyrolysis products to a crude unit for Example 8 are good feedstocks to be co-fed to a steam cracker for the production of ethylene with the recycled content. At least a portion, if not all, of the streams is fed to the steam cracker. The ethylene is processed in a polymerization unit to produce polyethylene resin containing some of the recycled polyethylene / polypropylene-derived materials, while the quality of the newly produced polyethylene is indistinguishable from virgin polyethylene manufactured entirely from virgin petroleum resources. The polyethylene resin with the recycled material is then further processed to produce various polyethylene products to suit consumer product needs.These polyethylene consumer products now contain chemically recycled polymer, while the quality of these polyethylene consumer products is indistinguishable from those manufactured entirely from virgin polyethylene polymer. These chemically recycled polymer products differ from mechanically recycled polymer products, whose qualities are inferior to those of polymer products manufactured from virgin polymers. Example 10: Production of Circular Normal Alpha Olefins and Petroleum Wax

[0086] The propane, butane, and naphtha streams produced via pyrolysis product co-feeding to a crude unit for Example 8 are good stocks of Petition 870260045608, dated 05 / 14 / 2026, page 33 / 77 27 / 30 feed to co-feed a steam cracker for the production of ethylene with recycled content. The ethylene is processed in an ethylene oligomerization unit to manufacture normal alpha olefins (NAO) with varying carbon chain lengths containing some recycled polyethylene / polypropylene-derived materials, while the quality of the fresh NAO is indistinguishable from virgin NAO manufactured entirely from virgin petroleum resources. These normal alpha olefins with recycled content are further converted to manufacture various chemicals such as polyalpha olefins (PAO), copolymerization reagent, etc. These chemicals now contain chemically recycled material from plastic waste, while the quality of the chemicals is indistinguishable from those manufactured entirely from virgin ethylene. Example 11: Production of Raw Paraffin and Paraffin Wax with Recycled Content

[0087] The pyrolysis wax from plastic waste (Sample E) is combined with the waxy heavy fraction of the normal alpha olefin (C22+) synthesis unit. The combined heavy fraction and the normal alpha olefin chain-weighted heavy fraction can then be passed to a wax hydrogenation zone to produce high-quality wax.

[0088] To examine the properties of recycled wax, Sample E, crude pyrolysis wax, was vacuum distilled to produce the 360°C+ (680°F+) fraction to yield crude pyrolysis paraffin, Sample J. Sample E was hydrogenated in a continuous fixed-bed unit containing a NiMo / Alumina catalyst at a reactor temperature of 335°C (635°F) and 8280 kPa (1200 psig) pressure. A liquid feed flow rate of 1.5 h⁻¹ relative to the catalyst bed volume and an H₂ / Hydrocarbon flow rate of 2500 scf / bbl were used to produce the hydrogenated product, Sample K, which is primarily wax. The hydrogenated product was vacuum distilled to produce the 343°C+(650°F)+ fraction as a hydrogenated pyrolysis paraffin wax, Sample L. The results are summarized in Table 7. Petition 870260045608, dated 05 / 14 / 2026, page 34 / 77 28 / 30 Table 7

[0089] Production of Crude Pyrolysis Paraffin and Paraffin Wax Sample E Sample J Crude Paraffin Sample K Sample L Paraffin Wax Crude Wax Sample E Cut as received 360°C (680 °F)+ Hydrotreated Sample E Sample K Specific Gravity at 16°C (60°F) 0.828 0.837 0.823 0.832 Simulated Distillation, °C (°F) 0.5% (Boiling Point 163 (325) 360 (680) 164 (328) 336 (636) Initial) 246 (475) 379 (715) 247 (477) 356 (672) 5% 285 (545) 386 (727) 286 (543) 363 (686) 10% 347 (656) 409 (768) 346 (654) 390 (734) 30% 389 (733) 430 (807) 388 (731) 414 (777) 50% 426 (798) 457 (854) 424 (796) 443 (829) 70% 479 (894) 499 (930) 477 (890) 487 (909) 90% 504 (939) 521 (970) 502 (935) 508 (947) 95% 573 (1064) 575 (1067) 567 (1053) 558 (1036) 99.5% (Final Boiling Point) Bromine Number, g / 100 g 14 6 0.08 - Contaminants Total S, ppm 6.3 <0.5 <5 - Total N, ppm 237 180 1.5 - Total Cl, ppm 4.7 1.9 <1 - Elemental Impurities Trace Fe, ppm 3.1 3.0 <0.57 - P, ppm 20.2 32.5 <2.3 - Petition 870260045608, dated 05 / 14 / 2026, page 35 / 77 29 / 30 Si, ppm 3.1 <2.7 <0.57 - Color & Physical State at room temperature - Light brown solid - White solid Flash Point, °C 96 216.5 127.5 203.5 Melting Point, °C 37.9 - - - Kinematic Viscosity at 100 °C, mm² / s - 4.3 - 3.8 Oil Content, % by weight - 18.7 - 34.4

[0090] Crude paraffin from the pyrolysis of plastic waste, Sample J shows a light brown color due to trace impurities in the sample. It contains trace amounts of nitrogen, phosphorus, iron, and silicon, but generally has good quality as a wax.

[0091] In hydrogenation, all trace impurities are completely removed. The resulting paraffin wax, Sample L, is white in color and of good quality as a wax. This example shows that high-quality, pure paraffin wax can be effectively produced from plastic waste containing predominantly polyethylene and polypropylene. Based on these results, the combined heavy fraction of NAO and wax from the pyrolysis of plastic waste is expected to produce quality wax after hydrogenation.

[0092] As used in this description, the word “comprises” or “comprising” is intended as an open-ended transition signifying the inclusion of the cited elements, but not necessarily excluding other uncited elements. The phrase “consists essentially of” or “consisting essentially of” is intended to signify the exclusion of other elements of any essential significance to the composition. The phrase “consisting of” or “consists of” is intended as a transition signifying the exclusion of all but the cited elements with the exception of only minor traces of impurities.

[0093] All patents and publications referenced herein are hereby incorporated by reference to the extent not inconsistent therewith. Petition 870260045608, dated 05 / 14 / 2026, page 36 / 77 30 / 30 It is understood that certain of the structures, functions, and operations described above in the embodiments described above are not necessary to practice the present invention and are included in the description simply for the completeness of an exemplary embodiment(s). Furthermore, it will be understood that specific structures, functions, and operations presented in the patents and publications referenced above may be practiced in conjunction with the present invention, but are not essential to its practice. Therefore, it should be understood that the invention may be practiced in a manner other than that specifically described without in fact diverging from the spirit and scope of the present invention as defined by the appended claims. Petition 870260045608, dated 05 / 14 / 2026, page 37 / 77

Claims

1 / 4 CLAIMS 1. Continuous process for converting plastic waste in recycling to normal alpha olefins, characterized in that it comprises: (a) selecting plastic waste containing polyethylene and / or polypropylene; (b) passing the plastic waste from (a) through a pyrolysis reactor to thermally crack at least a portion of the olefin waste and produce a pyrolyzed effluent; (c) separating the pyrolyzed effluent into expenditure gas, a naphtha / diesel fraction, a heavy fraction and charcoal; (d) passing the naphtha / diesel fraction to a crude unit in a refinery, with the volumetric flow of the naphtha / diesel fraction to the crude unit comprising up to 50% by volume or less of the total hydrocarbon flow to the crude unit; (e) recovering a direct-drive naphtha fraction (C5-C8) from the crude unit; (f) pass the direct-flow naphtha fraction to a steam cracker for the production of ethylene;and (g) pass ethylene to a normal alpha olefin synthesis unit to produce normal alpha olefins.; 2. Process according to claim 1, characterized in that the naphtha / diesel fraction of (c) is passed directly to the refinery crude unit and the contaminants are removed in a crude desalting unit.

3. Process according to claim 1, characterized in that the volumetric flow of naphtha / diesel comprises up to 20% by volume of the total hydrocarbon flow to the crude unit.

4. Continuous process for converting plastic waste in recycling for polyethylene polymerization characterized in that it comprises: (a) selecting plastic waste containing polyethylene and / or polypropylene; (b) passing the plastic waste from (a) through a pyrolysis reactor to thermally crack at least a portion of the olefin waste and produce a pyrolyzed effluent; (c) separating the pyrolyzed effluent into excretion gas, a naphtha / diesel fraction, a heavy fraction and charcoal; (d) passing the naphtha / diesel fraction to a crude unit in a refinery, with the volumetric flow of the naphtha / diesel fraction to the crude unit comprising up to 50% by volume or less of the total hydrocarbon flow to the crude unit; (e) recover the direct conduction naphtha fraction (C5-C8) from the crude unit;(f) passing the direct-drive naphtha fraction to a steam cracker for the production of ethylene; (g) passing the ethylene to the normal alpha olefin synthesis unit to produce normal alpha olefins and recover a heavy fraction of the normal alpha olefin (C22+) stream; (h) combining the heavy fraction from (c) with the heavy fraction of the normal alpha olefin (C22+) stream from (g); and (i) passing the combined heavy fraction and the heavy fraction of the normal alpha olefin stream from (g) to a wax hydrogenation zone to produce wax.

5. Process according to claim 4, characterized in that the naphtha / diesel fraction of (c) is passed directly to the refinery crude unit and the contaminants are removed in a crude desalting unit.

6. Process according to claim 4, characterized in that the ethylene produced in (f) is subsequently polymerized to prepare polymerized ethylene, and polyethylene products are prepared from the polymerized ethylene.

7. Process according to claim 4, characterized in that naphtha / diesel / heavy atmospheric gas oil is recovered from the crude unit and further processed in the refinery to clean gasoline, diesel or jet fuel.

8. Process according to claim 1 or 4, characterized by the fact Petition 870260045608, dated 05 / 14 / 2026, page 39 / 77 3 / 4 that the plastic wastes selected in (a) are from groups 2, 4 and / or 5 of the plastics classification.

9. Process according to claim 4, characterized in that the naphtha / diesel flow comprises up to 20% by volume of the total hydrocarbon flow to the crude unit.

10. Continuous process for converting plastic waste in recycling for polyethylene polymerization, characterized in that it comprises: (a) selecting plastic waste containing polyethylene and / or polypropylene; (b) passing the plastic waste from (a) through a pyrolysis reactor to thermally crack at least a portion of the olefin waste and produce a pyrolyzed effluent; (c) separating the pyrolyzed effluent into excretion gas, a naphtha / diesel fraction, a heavy fraction and charcoal; (d) passing the naphtha / diesel fraction to a crude unit in a refinery, with the volumetric flow of the naphtha / diesel fraction to the crude unit comprising up to 50% by volume or less of the total hydrocarbon flow to the crude unit; (e) recovering a portion of a propane and butane (C3-C4) fraction from the crude unit; (f) pass the C3-C4 fraction recovered from (e) to a steam cracker for the production of ethylene;(g) combine the heavy fraction of (c) with a heavy (C22+) fraction of normal alpha olefin stream; and (h) pass the combined heavy fraction and the heavy (C22+) fraction of normal alpha olefin stream from (g) to a wax hydrogenation zone to produce wax.

11. Process according to claim 10, characterized in that the naphtha / diesel fraction of (c) is passed directly to the refinery crude unit and the contaminants are removed in a crude desalting unit.

12. Process according to claim 10, characterized in that Petition 870260045608, dated 05 / 14 / 2026, page 40 / 77 4 / 4 that the ethylene produced in (f) is subsequently polymerized and polyethylene products are prepared from the polymerized ethylene.

13. Process according to claim 10, characterized in that naphtha / diesel / heavy atmospheric gas oil is recovered from the crude unit and further processed in the refinery to clean gasoline, diesel or jet fuel.

14. Process according to claim 10, characterized in that the plastic wastes selected in (a) are from plastic classification groups 2, 4 and / or 5.

15. Process according to claim 1, characterized in that it further comprises: (h) passing the heavy fraction in (c) to a wax hydrogenation zone. Petition 870260045608, dated 05 / 14 / 2026, p. 41 / 77

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