Continuous process for converting plastic waste in recycling to polyethylene polymerization.

Abstract

CIRCULAR ECONOMY FOR PLASTIC WASTE TO POLYETHYLENE VIA REFINERY FCC AND ALKYLATION UNITS. A continuous process is provided for converting recycled plastic waste to polyethylene polymerization. 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 expenditure gas, a pyrolysis oil and optionally wax comprising a fraction of naphtha / diesel and heavy and coal. The pyrolysis oil and wax are passed to a refinery FCC unit from which a C3-C5 olefin mixture fraction of liquid petroleum gas / paraffin is recovered.The C3-C5 olefin mixture fraction of liquid petroleum gas / paraffin is passed to a refinery alkylation unit, with a propane and butane fraction recovered from the alkylation unit. The propane and butane fraction is then passed to a steam cracker for the production of ethylene. In another embodiment, a naphtha fraction (C5-C8) is recovered from the alkylation unit and passed to the steam cracker. In yet another embodiment, a propane / propylene fraction (C3-C3=) is recovered from the FCC and passed to the steam cracker.

Description

1 / 29 “CONTINUOUS PROCESS FOR CONVERTING PLASTIC WASTE INTO POLYETHYLENE POLYMERIZATION IN RECYCLING” 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 liquid fuel components using standard refining techniques. (US Patent No. 6,143,940) Petition 870260045610, dated 05 / 14 / 2026, page 8 / 75 Patent No. 2 / 29 discloses a procedure for converting waste plastics into heavy wax compositions. U.S. Pat. No. 6,150,577 discloses a process for converting waste plastics into lubricating oils. EP0620264 discloses a process for producing lubricating oils from waste or virgin polyolefins by thermally cracking the waste in a fluidized bed to form a waxy product, optionally using 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

[0007] A continuous process is provided for converting plastic waste into Petition 870260045610, dated 05 / 14 / 2026, page 9 / 75 3 / 29 Recycling for polyethylene polymerization. The process involves 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 pyrolysis oil, and optionally pyrolysis wax comprising a fraction of naphtha / diesel and heavy metals 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 polyethylene. Thus, the pyrolysis oil and wax are passed to a refinery FCC unit from which a C3-C5 olefin mixture fraction of liquid petroleum gas / paraffin is recovered. The C3-C5 olefin mixture fraction of liquid petroleum gas / paraffin is passed to a refinery alkylation unit from which a propane fraction and a butane fraction are recovered. The propane or butane or the combined propane and butane fraction is then 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 flow volume of pyrolysis oil and paraffin generated from the pyrolysis of plastic waste to the refinery units may comprise any practical or accommodative volume percentage of the total flow to the refinery units. Generally, the flow of pyrolysis oil and paraffin 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 flow of pyrolysis oil and paraffin is an amount up to about 20% by volume of the total flow.

[0010] 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 then passing the plastic waste through a pyrolysis reactor to crack it. Petition 870260045610, dated 05 / 14 / 2026, page 10 / 75 4 / 29 Thermally, at least a portion of the olefin residues is decomposed to produce a pyrolyzed effluent. The pyrolyzed effluent is separated into expendia gas, an oil and wax pyrolysis comprising a naphtha / diesel and heavy fraction, and charcoal. The oil and wax pyrolysis is passed to a refinery FCC unit from which a C3-C5 olefin mixture fraction of liquid petroleum gas / paraffin is recovered. The C3-C5 olefin mixture fraction of liquid petroleum gas / paraffin is passed to a refinery alkylation unit from which a naphtha fraction (C5-C8) is recovered. The naphtha fraction is then passed to a steam cracker for the production of ethylene.

[0011] In another embodiment, the C3 olefin / paraffin mixture, recovered from an FCC unit, is then passed to a steam cracker for the production of ethylene. The C3 olefin / paraffin mixture is preferably fed to the high-efficiency distillation column of the steam cracking unit where pure propane is separated and then fed to the steam cracker reactor.

[0012] Among other factors, it was found that by adding refinery operations, waste pyrolysis oil and wax can be improved to higher value products such as gasoline and diesel. Also, by adding refinery operations, it was found that clean naphtha (C5-C8) or LPG C3-C4 or LPG C3 (liquefied petroleum gas) can be efficiently and effectively produced from waste pyrolysis oil and wax for the production of final polyethylene polymer. Positive economies are realized for the overall process from recycled plastics to a polyethylene product with product quality identical to that of virgin polymer. BRIEF DESCRIPTION OF THE DRAWINGS

[0013] FIG 1 represents the current practice of pyrolyzing plastic waste to produce fuel or wax (base case).

[0014] FIG. 2 represents a present process for establishing a circular economy for plastic waste.

[0015] FIG. 3 represents the classification of plastic type for recycling of Petition 870260045610, dated 05 / 14 / 2026, page 11 / 75 5 / 29 plastic waste. DETAILED DESCRIPTION

[0016] In the present process, a method is provided for recycling waste polyethylene and / or polypropylene back into virgin polyethylene to establish a circular economy by combining 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.

[0017] 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.

[0018] 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 (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 structures. 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 Petition 870260045610, dated 05 / 14 / 2026, page 12 / 75 6 / 29 Substantially linear polymer with significant numbers of short branches, usually made by copolymerization of ethylene with short-chain alpha-olefins.

[0019] 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 branches. High-density polyethylene (HDPE) is manufactured at relatively low pressure (10 to 80 atm) and temperature of 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 fabrication is done via a flow 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 for HDPE except for the copolymerization of ethylene with short-chain alpha-olefins (1-butene or 1-hexene).

[0020] Currently, only a small portion of spent polyethylene products is collected for recycling efforts due to the inefficiencies discussed above.

[0021] FIG. 1 shows a diagram of the pyrolysis of fuel or wax from waste plastic that is commonly operated in the 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. A distillation unit in the pyrolysis unit separates the 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., it forms paraffin wax upon cooling to temperature). Petition 870260045610, dated 05 / 14 / 2026, page 13 / 75 7 / 29 environment). The wax can be separated from the heavy fraction 6 and sold to wax markets.

[0022] 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 polymers (naphtha or C3-C4 or just C3 for ethylene cracker), high-quality gasoline and diesel fuel and / or high-quality base oil.

[0023] 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 or just C3 can be fed to the cracker with steam. The ethylene is then polymerized to create polyethylene.

[0024] By adding refinery operations to enhance pyrolysis residue oil and wax into higher value products (gasoline, jet and diesel) and to produce clean LPG and naphtha for the steam cracker for the production of final polyethylene polymer, one is able to create positive economies for the overall process from recycled plastics to polyethylene product with identical quality to that of virgin polymer.

[0025] 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 large quantities for blending into transportation fuels. It has been found that by having these products go through refinery units, the contaminants can be captured in pretreatment units and their negative impacts reduced. The fuel components can be further enhanced with appropriate refinery units with chemical conversion processes, with the final transportation fuels produced by the integrated process being of higher quality and meeting fuel quality requirements. The present process will enhance the wax in valuable gasoline and diesel. The process Petition 870260045610, dated 05 / 14 / 2026, page 14 / 75 The integrated 8 / 29 will generate a much cleaner naphtha or LPG stream as steam cracker feedstock for ethylene generation and polyethylene production. These grade-grade productions within specifications allow for feasible “cycle economy” for plastics recycling.

[0026] 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.

[0027] 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 pyrolysis 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 in the pyrolysis unit 23, 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.

[0028] The pyrolysis unit may be located near the plastic waste collection site, which may be far from a refinery, near a refinery, 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 the pyrolysis unit be located within the plastic waste collection site or inside the refinery.

[0029] The preferred starting material for the present process is graded plastic waste containing predominantly polyethylene and polypropylene. Petition 870260045610, dated 05 / 14 / 2026, page 15 / 75 9 / 29 (recycling classification of plastics types 2, 4 and 5). The pre-sorted 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 recycling plastic waste. Classification types 2, 4 and 5 are high-density polyethylene, polyethylene and low-density polypropylene, respectively. Any combination of polyethylene and polypropylene plastic waste can be used. For the present process, at least some of the polyethylene plastic waste is preferred.

[0030] 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%.

[0031] Washing plastic waste removes metallic contaminants such as sodium, calcium, magnesium, 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 less than 5 ppm.

[0032] If washing does not remove metals, non-metallic contaminants and halide impurities adequately, then a separate protective bed may Petition 870260045610, dated 05 / 14 / 2026, p. 16 / 75 10 / 29 can be used to remove metals and non-metallic contaminants.

[0033] 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 primarily 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.

[0034] FIG. 2 shows the present integrated process where all the pyrolysis oil (naphtha / diesel fraction and heavy fraction) is sent to a fluid catalytic cracking (FCC) unit 28.

[0035] The fluid catalytic cracking (FCC) process is widely used in the refining industry for the conversion of atmospheric gas oil, vacuum gas oil, atmospheric waste, and heavy stocks recovered from other refinery operations into high-octane gasoline, mild fuel oil, heavy fuel oil, olefin-rich mild gas (LPG), and coke. FCC uses a high-activity zandolytic catalyst to crack heavy hydrocarbon molecules at a reactor temperature of 510 to 532°C (950 to 990°F) in a lift with a short contact time of a few minutes or less. The LPG product streams containing olefins (propylene, butylene) are usually further improved to manufacture alkylated gasoline or to be used in the manufacture of chemicals. A conventional FCC unit is used.

[0036] The refinery will generally have its own hydrocarbon feed flowing through the refinery units. The flow volume of pyrolysis oil and wax generated from the pyrolysis of plastic waste to the refinery units, here an FCC unit, may comprise any % of the total flow volume. Petition 870260045610, dated 05 / 14 / 2026, p. 17 / 75 11 / 29 practical or accommodative for refinery units. Generally, the flow of the pyrolysis oil and wax fraction generated from the pyrolysis of plastic waste, for practical reasons, can be up to about 50% by volume of the total flow, i.e., of the refinery flow and the pyrolysis flow. In one embodiment, the pyrolysis oil and wax flow is an amount up to about 20% by volume of the total flow. In another embodiment, the pyrolysis oil and wax flow is an amount up to about 10% by volume of the total flow. About 20% by volume has been found to be a quantity that is quite practical in its impact on the refinery while also providing excellent results and being an amount that can be accommodated. The amount of pyrolysis oil generated from pyrolysis can naturally be controlled so that the fraction passed to the refinery units provides the desired % by volume of the flow.

[0037] The cracking of liquid oil from pyrolysis combined with petroleum-derived oil in an FCC unit produces liquefied petroleum gas (LPG) from a C3-C5 olefin / paraffin mixture 29, as well as gasoline and a heavy fraction 30. The C3-C4 olefin / paraffin mixture 29 from the FCC plant is sent to an alkylation plant 31 which produces pure propane 32 and n-butane 33 streams.

[0038] An alkylation process combines soft olefins (propylene, butylene, typically from the FCC unit) with isobutane to produce highly branched paraffinic fuel, alkylated gasoline. Alkylated gasoline is a clean-burning, high-octane, low-sulfur, low-RVP gasoline blend component that does not contain olefinic or aromatic compounds, thus it is a highly desirable gasoline blend component. Conventional alkylation processes use a sulfuric acid catalyst operating at a reactor temperature of -1 to 16°C (30 to 60°F) or a hydrofluoric acid catalyst operating at a reactor temperature of 32 to 35°C (90 to 95°F). A conventional alkylation process can be used.

[0039] The pure propane and n-butane streams from the alkylation unit 31 are excellent feeds to a steam cracker 34 for manufacturing ethylene. The alkylation unit 31 also produces clean, high-octane gasoline 35. The heavy fraction 30 from the FCC unit is sent to the appropriate refinery units 36 for upgrading to clean gasoline and diesel. A product of Petition 870260045610, dated 05 / 14 / 2026, page 18 / 75 12 / 29 FCC gasoline can also be recovered from the FCC unit. The ethylene 37 manufactured in the steam cracker 34 is passed through a polymerization unit 40 to produce polyethylene, with the polyethylene polymer used for polyethylene products 41 to suit the needs of consumer products.

[0040] Alternatively, instead of sending the C3-C4 olefin / paraffin mixture, recovered from an FCC unit, to an alkylation unit, at least a portion, if not all, of the C3 olefin / paraffin mixture from FCC 45 is passed directly to a steam cracker 34. The C3 stream is fed to a steam cracker distillation section 34 to separate it into propane and propylene. Then, propane is fed to the steam cracker reactor for ethylene production.

[0041] The steam cracker and ethylene polymerization unit is preferably located close to the refinery so that feedstocks (propane, butane, naphtha or propane / propylene mixture) can be transferred via pipeline. For a petrochemical plant located further away from the refinery, the feedstock can be delivered via truck, barge, railcar or pipeline.

[0042] In another embodiment, a fraction of naphtha (C5-C8) 38 is recovered from the alkylation unit 31. This stream 38 can also be fed to a steam cracker 34 for the production of ethylene 37 and subsequent ethylene polymerization 40. Polyethylene products 41 can then be manufactured from the polyethylene.

[0043] The benefits of a circular economy and an effective and efficient recycling campaign are realized by this integrated process.

[0044] 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

[0045] The pyrolysis oil and wax samples were obtained from commercial sources and their properties are summarized in Table 1. These samples of Petition 870260045610, dated 05 / 14 / 2026, page 19 / 75 13 / 29 pyrolysis units 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, optionally wax and charcoal product. The top gas stream from the pyrolysis unit containing thermally cracked hydrocarbon was 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

[0046] Properties of Oil and Wax as Obtained from the Pyrolysis of Waste Plastics 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) Petition 870260045610, dated 05 / 14 / 2026, page 20 / 75 14 / 29 99.5% (Final Boiling Point) Carlo-Erba Hydrocarbon Analysis 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, % by vol 37.7 27 52.5 53.1 44.6 Total Paraffins, % by vol Contaminants Total S, ppm 48 29 7.8 99 6.3 Total N, ppm 751 1410 318 353 237 Total Cl, ppm 113 62 41 70 4.7 O 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 Petition 870260045610, dated 05 / 14 / 2026, page 21 / 75 15 / 29 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

[0047] 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).

[0048] 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.

[0049] The pyrolysis product is a fairly pure hydrocarbon composed mostly of carbon and hydrogen. The molar ratio of hydrogen to carbon varies from 1.7 to almost 2.0. The bromine number is in the range of 14 to 60, indicating varying degrees of unsaturation originating from olefins and aromatics. The aromatic content is in the range of 5 to 23% by volume, with a higher severity unit producing more aromatics. Depending on the process conditions of the unit Petition 870260045610, dated 05 / 14 / 2026, page 22 / 75 16 / 29 of pyrolysis, the pyrolysis products have a paraffin content ranging from mid-20% by volume to mid-50% by volume. The pyrolysis product contains a substantial amount of olefins. Samples A and B, pyrolysis oil produced under more severe conditions such as higher pyrolysis temperature and / or longer residence time, 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 severe 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.

[0050] The following Examples 2 to 5 present the evaluation of pyrolysis oil from waste plastics for transport fuel. Example 2: Fractionation of Pyrolysis Oil for Evaluation as a Transportation Fuel

[0051] 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

[0052] Pyrolysis Oil Distillation into Fuel Fractions Petition 870260045610, dated 05 / 14 / 2026, page 23 / 75 17 / 29 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

[0053] Sample F, a pyrolysis oil cut for the boiling range of fuel gasoline, was evaluated to estimate its potential for use as fuel gasoline. Sample F has the carbon number range of C5 to C12, typical of fuel gasoline.

[0054] 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

[0055] Evaluation of the Naphtha Fraction of Pyrolysis Oil for Fuel Gasoline Washed Gum Stability, RON MON Petition 870260045610, dated 05 / 14 / 2026, page 24 / 75 18 / 29 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

[0056] 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.

[0057] We also examined the potential for combining pyrolysis gasoline cut-off 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.

[0058] 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 870260045610, dated 05 / 14 / 2026, page 25 / 75 19 / 29 pyrolysis in hydrocarbon that reaches the property targets of gasoline fuel. Example 4: Evaluation of Pyrolysis Oil Cut-Off for Jet Fuel

[0059] 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.

[0060] 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.

[0061] 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

[0062] 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

[0063] 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 870260045610, dated 05 / 14 / 2026, page 26 / 75 20 / 29 Example 5: Evaluation of Pyrolysis Oil Cut-Off for Diesel Fuel

[0064] 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.

[0065] 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.

[0066] 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

[0067] 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

[0068] These results indicate that pyrolysis oil as such is completely Petition 870260045610, dated 05 / 14 / 2026, page 27 / 75 21 / 29 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 Product to FCC Unit or FCC Pre-Treaper Unit

[0069] 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 high 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.

[0070] 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 an FCC feed treatment unit before the FCC unit so that the bulk of the impurities are effectively removed by the pre-treater.

[0071] By feeding the entire pyrolysis feedstock to an FCC unit as shown in Figure 2 or to an FCC pre-treatment unit prior to the FCC unit, the pyrolysis oil and wax are converted into falloff gas, LPG paraffins and olefins, FCC gasoline, and heavy hydrocarbon components. FCC gasoline is a valuable gasoline blend component. LPG paraffins and olefins are further processed in an alkylation unit to manufacture alkylated gasoline, another valuable gasoline blend component. Alternatively, the C3 propane / propylene blend is separated from the FCC unit and purified via FCC light end recovery and gas treatment units and then fed to a steam cracker. The heavy fractions, soft cycle oil (LCO) and heavy cycle oil (HCO), are Petition 870260045610, dated 05 / 14 / 2026, page 28 / 75 22 / 29 additionally converted in subsequent conversion units including jet hydrotreating unit, diesel hydrotreating unit, hydrocracking unit and / or coking unit to manufacture more gasoline, jet and diesel fuel with satisfactory product properties.

[0072] The following Examples 7 and 8 demonstrate the conversion of pyrolysis product from waste plastic into quality transportation fuel in a refinery conversion unit, using an FCC unit as an example. Example 7: Conversion of Pyrolysis Oil to FCC

[0073] To study the impact of co-processing pyrolysis oil from waste plastics 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% ​​by volume of pyrolysis oil with VGO and pure pyrolysis oil were compared with those of pure VGO feed.

[0074] 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)), mild 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. Petition 870260045610, dated 05 / 14 / 2026, page 29 / 75 23 / 29 Table 6

[0075] Evaluation of Pyrolysis Oil Co-feeding for FCC Feed 100% VGO Combination of 20 / 80% by vol, Sample A / VGO Combination of 20 / 80% by vol, Sample C / VGO 100% of Sample A 100% of Sample C 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 O, ppm 27 30 33 50 21 Total N, ppm Yields Coke, % 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 Petition 870260045610, dated 05 / 14 / 2026, page 30 / 75 24 / 29 Gasoline, % by weight LCO, % by weight HCO, % by weight 53.53 12.89 5.81 55.75 12.23 4.63 55.46 11.93 4.98 62.53 10.37 1.82 61.75 8.03 1.50 Octane Rating*** 88.05 84.57 82.79 73.75 75.41

[0076] *: Conversion - conversion of the fraction 221 °C+ to 221°C-(430oF+ to 430oF-)

[0077] **: Level of N and O impurities in the whole liquid product in the boiling range of fuels by GC x GC, ppm

[0078] ***: Octane number, (R+M) / 2, was estimated from the detailed FCC gasoline hydrocarbon GC.

[0079] 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 mild, 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 mild reduction in coke and dry gas yields, a mild increase in gasoline yield, and a mild 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.

[0080] The FCC unit cracks pyrolysis oil into hydrocarbons in the fuel range, reduces impurities, and isomerizes n-paraffins to isoparaffins. All these chemistries improve the fuel properties of the pyrolysis oil and wax. By co-feeding the pyrolysis oil through the FCC process unit with a zeolite catalyst, oxygen and nitrogen impurities in the range are removed. Petition 870260045610, dated 05 / 14 / 2026, page 31 / 75 25 / 29 fuel has been substantially reduced, from about 300 to 1400 ppm of N to about 30 ppm of N and from about 250 to 540 ppm of O to about 60 to 80 ppm of O. The hydrocarbon composition of all these co-feed products is well within the typical FCC gasoline range.

[0081] 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: Co-processing of Pyrolysis Wax at the FCC

[0082] To study the impact of co-processing pyrolysis wax from waste plastic for FCC, a series of laboratory tests were conducted with Sample E and VGO. The FCC performance of the combination of 20% pyrolysis wax with VGO and pure pyrolysis wax was compared with that of pure VGO feed, similar to Example 7. The results are summarized below in Table 7. Table 7

[0083] Evaluation of Co-feeding Pyrolysis Wax for FCC Feed 100% VGO Combination of 20 / 80% by vol, Sample E / VGO 100% Sample E Cat / Oil, w / w 6.5 6.5 6.5 Conversion, % by weight* 82.75 84.17 91.31 Yields Coke, % by weight 4.78 4.76 4.26 Total dry gas, % by weight Hydrogen 2.11 0.16 2.05 0.14 1.79 0.07 Petition 870260045610, dated 05 / 14 / 2026, page 32 / 75 26 / 29 Methane 0.69 0.67 0.58 Ethane 0.44 0.43 0.37 Ethylene 0.78 0.77 0.73 LPG Total, % 21.71 23.15 31.79 by weight Propane 1.30 (87) 1.93 2.28 Propylene 5.54 5.98 8.59 n-Butane 1.65 1.74 2.15 Isobutane 6.91 7.25 8.88 C4 Olefins 5.74 6.25 9.89 Gasoline, % 54.16 54.21 53.47 wt LCO, % 12.42 11.59 6.71 wt HCO, % in 4.83 4.24 1.99 weight Index 89.95 88.38 83.52 Octane**

[0084] *: Conversion - conversion of the fraction from 221°C (430°F+) to 221°C (430°F-)

[0085] **: Octane number, (R+M) / 2, was estimated from detailed FCC gasoline hydrocarbon GC.

[0086] The results in Table 7 show that co-feeding up to 20% by volume of pyrolysis wax only makes the changes in FCC unit performance very mild, indicating that co-processing pyrolysis wax up to 20% is easily practicable. The 20% by volume combination of Sample E led to a very mild reduction to no change in coke and dry gas yields, a notable increase in LPG olefin yield, a very mild increase in gasoline yield, and a mild decrease in LCO and HCO, all of which are favorable in most situations. With the paraffinic nature of pyrolysis wax, the 20% combination of Sample E decreased the Octane Number slightly by 1.5 points. With the Petition 870260045610, dated 05 / 14 / 2026, page 33 / 75 27 / 29 Flexibility of the blend at the refinery, this shortfall in the Octane Index can be easily offset with minor blend adjustments.

[0087] The FCC round of 100% pyrolysis wax showed a substantial increase in conversion and Octane Index rate by 6. This shows that co-processing pyrolysis wax is preferable to processing 100% pyrolysis wax. Example 9: Feeding LPG Olefins from the FCC Unit, which co-processed products from the pyrolysis of plastic waste, to the Alkylation Unit of the Refinery.

[0088] Feeding pyrolysis oil to a refinery FCC unit produces a substantial amount of C3-C5 olefins with a recycled content. Streams containing only C4, C3-C4, or C3-C5 recycled olefins are separated from the light-end recovery FCC units and then fed to an alkylation unit. The reaction of LPG olefins and isobutane in the alkylation reactor produces propane, butane, and alkylated gasoline. Alkylated gasoline is a very valuable gasoline blending component. The clean propane, butane, and naphtha streams from the alkylation unit are valuable feedstocks for a steam cracker. Example 10: Feeding Recycled C3-C4 and / or Naphtha to the Steam Cracker for Ethylene Production, Followed by Polyethylene Resin Production and Polyethylene Consumer Products

[0089] The propane, butane, and naphtha streams produced via co-feeding pyrolysis products to an FCC unit and then to an alkylation unit for Examples 8 and 9 are good feed stocks for a co-fed steam cracker for the production of ethylene with a recycling content. Alternatively, the C3 propane and propylene stream is recovered from the FCC unit and then purified in the FCC light-end recovery units and then co-fed to a steam cracker for the production of ethylene with a recycling content. At least a portion, if not all, of the streams are fed to the steam cracker. The ethylene is then Petition 870260045610, dated 05 / 14 / 2026, page 34 / 75 28 / 29 processed for a polymerization unit to produce polyethylene resin containing some recycled polyethylene / polypropylene derivative materials, while the quality of the newly produced polyethylene is indistinguishable from that of 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 needs. These consumer polyethylene products now contain chemically recycled, circular polymer, while the quality of the consumer polyethylene products is indistinguishable from those manufactured entirely from virgin polyethylene polymer. These chemically recycled polymer products are different from mechanically recycled polymer products, whose qualities are inferior to polymer products manufactured from virgin polymers.

[0090] 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.

[0091] All patents and publications referenced herein are hereby incorporated by reference to the extent not inconsistent therewith. It shall be 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 shall 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 this one. Petition 870260045610, dated 05 / 14 / 2026, page 35 / 75 29 / 29 specifically described without actually diverging from the spirit and scope of the present invention as defined by the appended claims. Petition 870260045610, dated 05 / 14 / 2026, p. 36 / 75

Claims

1 / 4 CLAIMS 1. 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 polyolefin waste and produce a pyrolyzed effluent; (c) separating the pyrolyzed effluent into expenditure gas, charcoal and a pyrolysis oil comprising a naphtha / diesel fraction and a heavy fraction, and wax; (d) passing the pyrolysis oil and wax from (c) to a refinery FCC unit with the volume flow of wax and pyrolysis oil to the refinery FCC unit comprising up to 50% by volume or less of the total hydrocarbon feed to the FCC unit; (e) recover a liquid C3-C5 paraffin / olefin mixture fraction from petroleum gas from the FCC unit;(f) pass the liquid C3-C5 paraffin / olefin mixture fraction from petroleum gas to a refinery alkylation unit; (g) recover a propane fraction and a butane fraction from the alkylation unit; and (h) pass the propane fraction or butane fraction or a combination of propane and butane fractions to a steam cracker for the production of ethylene.

2. Process according to claim 1, characterized in that a fraction of gasoline and heavy fuels is recovered from the FCC unit of the refinery.

3. Process according to claim 1, characterized in that an alkylated gasoline fraction is recovered from the refinery alkylation unit.

4. Process according to claim 1, characterized in that Petition 870260045610, dated 05 / 14 / 2026, page 37 / 75 2 / 4 the ethylene produced in (h) is subsequently polymerized, and polyethylene products are prepared from polymerized ethylene.

5. Process according to claim 2, characterized in that the gasoline fraction recovered from the refinery's FCC unit is combined with an alkylated gasoline fraction recovered from the alkylation unit.

6. Process according to claim 1, characterized in that the volume flow of pyrolysis feed to the refinery FCC unit is up to about 20% by volume of the total hydrocarbon feed to the FCC unit.

7. 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 expenditure gas, charcoal and a pyrolysis oil comprising a naphtha / diesel fraction and a heavy fraction, and wax; (d) passing the pyrolysis oil and wax from (c) to a refinery FCC unit with the volume flow of wax and pyrolysis oil to the refinery FCC unit comprising up to 50% by volume or less of the total hydrocarbon feed to the FCC unit; (e) recovering a C3-C5 paraffin / olefin mixture fraction from liquid petroleum gas from the FCC unit;(f) pass the C3-C5 paraffin / olefin mixture fraction from liquid petroleum gas to a refinery alkylation unit; (g) recover a naphtha fraction from the alkylation unit; and (h) pass the naphtha fraction to a steam cracker for the production of ethylene. Petition 870260045610, dated 05 / 14 / 2026, page 38 / 75 3 / 4; 8. Process according to claim 7, characterized in that a gasoline and heavy fraction are recovered from the FCC unit of the refinery.

9. Process according to claim 7, characterized in that an alkylated gasoline fraction is recovered from the refinery alkylation unit.

10. Process according to claim 8, characterized in that the gasoline fraction recovered from the refinery's FCC unit is combined with an alkylated gasoline fraction recovered from the alkylation unit.

11. Process according to claim 7, characterized in that the ethylene produced in (h) is subsequently polymerized, and polyethylene products are prepared from the polymerized ethylene.

12. Process according to claim 7, characterized in that the volume flow of the pyrolysis stream to the refinery FCC unit is up to about 20% by volume of the total feed to the FCC unit.

13. 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, charcoal and a pyrolysis oil comprising a naphtha / diesel fraction and a heavy fraction; (d) passing the pyrolysis oil to a refinery FCC unit with the pyrolysis oil volume flow to the refinery FCC unit comprising up to 50% by volume or less of the total hydrocarbon feed to the FCC unit; (e) recovering a C3 olefin mixture fraction from liquid petroleum gas / paraffin from the FCC unit; Petition 870260045610, dated 05 / 14 / 2026, page.39 / 75 4 / 4 (f) pass the C3 olefin / paraffin fraction to a steam cracker for the production of ethylene.

14. Process according to claims 1, 7 and 13, characterized in that the plastic wastes selected in (a) are from plastic classification groups 2, 4, and / or 5. Petition 870260045610, dated 05 / 14 / 2026, p. 40 / 75

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