BACKGROUND

[0001] Thermoplastic hydrocarbon resins are one of the crucial components of adhesives for hygiene, packaging, automotive, woodworking and other applications. In many cases, these resins are formed from fossil fuel feedstocks, such as natural gas, petroleum liquids, and/or coal. Because fossil fuels are commonly used to produce hydrocarbon resins, there can be a substantial “carbon footprint” associated with their production. It is well known that products having large carbon footprints are becoming increasing undesirable from an environmental and economic standpoint.

[0002] Thus, a need exists for methods of producing hydrocarbon resins with existing equipment and processes and without the need to invest in additional and expensive equipment in order to establish a recycle content in the manufacture of hydrocarbon resins.

BRIEF SUMMARY OF THE DRAWINGS

[0003] Figure 1 shows one embodiment of the invention to make one or more recycle content compositions, including, for example, recycle content hydrocarbon resins, recycle content adhesives, and recycle content end products that include an adhesive

[0004] Figure 2 shows one embodiment of the invention where the hydrocarbon waste material introduced into the pyrolysis facility can include waste plastic, biowaste, and combinations thereof

[0005] Figure 3 shows a diagram of the main steps/zones of a pyrolysis facility according to one or more embodiments of the present invention [0006] Figure 4 shows an exemplary cracking facility for converting a cracker feed stream including, for example, pyrolysis effluent and/or bio-naphtha, into one or more recycle content hydrocarbon streams.

[0007] Figure 5 shows one embodiment of the invention where the cracker feed is introduced into a cracking furnace, wherein the hydrocarbon components therein are thermally cracked to form lighter hydrocarbons, including olefins such as ethylene, propylene, and/or butadiene, as well as benzene, toluene, xylene (BTX) and C9 and heavier hydrocarbon components [0008] Figure 6 shows one embodiment of the invention where the furnace effluent may be introduced into a fractionation/quenching zone, wherein the stream can be cooled and at least partially condensed.

[0009] Figure 7 shows one embodiment of the invention where an exemplary C9 resin production facility for converting a hydrocarbon feed stream into a C9 hydrocarbon resin is provided.

DETAILED DESCRIPTION

[0010] Turning initially to FIG. 1 , below, the main steps of a process for making and using a recycle content hydrocarbon resin are shown. It should be understood that FIG. 1 depicts one exemplary embodiment of the present technology. Certain features depicted in FIG. 1 may be omitted and/or additional features described elsewhere herein may be added to the system depicted in FIG. 1 . As discussed below in greater detail, the process of FIG. 1 may be used to make one or more recycle content compositions, including, for example, recycle content hydrocarbon resins, recycle content adhesives, and recycle content end products that include an adhesive.

[0011] As shown in FIG. 1 , the main steps of the process can include pyrolysis of hydrocarbon waste material in a pyrolysis step/facility, cracking of a pyrolysis effluent stream and/or a stream of bio-naphtha in a cracking step/facility, optional treatment of the cracker effluent in a treatment step/facility, production of a hydrocarbon resin in a hydrocarbon resin production step/facility, production of an adhesive in an adhesive production step/facility, and production of an end product (that includes an adhesive) in an end product production step/facility. Although shown as including all of these steps or zones, it should be understood that processes and facilities according to embodiments of the present technology can include at least two, three, four, five, or all of these steps/zones. [0012] In one or more embodiments, at least one of the hydrocarbon resin, adhesive, and end product can include recycle content directly or indirectly derived from a waste material including, for example, a hydrocarbon waste material such as waste plastic or bio-naphtha. As used herein, the term “directly derived” means having at least one physical component originating from the waste material, while “indirectly derived” means having an assigned recycle content that i) is attributable to the waste material, but ii) that is not based on having a physical component originating from the waste material. The determination of whether a recycle content composition or product is derived directly or indirectly from recycled waste is not on the basis of whether intermediate steps or entities do or do not exist in the supply chain, but rather whether at least a portion of the recycle content composition or product that is fed to the reactor for making a product can be traced to an recycle content composition or product made from recycled waste.

[0013] Although described herein as being part of a single facility, it should be understood that two or more of the pyrolysis step/facility, the cracking step/facility, the hydrocarbon resin production step/facility, the adhesive production step/facility, and the end product production step/facility may be located in different geographical locations and/or be operated by different commercial entities. Each of the pyrolysis, cracking, resin production, adhesive production and end product production steps/zones may be operated by the same entity or, more likely, two or more of the pyrolysis, cracking, resin production, adhesive production, and end product production steps/zones may be operated by different entities.

[0014] In one or more embodiments, at least one of the pyrolysis, cracking, resin production, adhesive production, and end product production steps may be performed in a commercial-scale facility capable of processing significant volumes of waste material. As used herein, the term “commercial-scale facility” refers to a facility having an average annual feed rate of at least 500 pounds per hour, averaged over one year.

[0015] In addition, two or more facilities used to carry out the processing steps shown in FIG. 1 may also be co-located with one another. In one or more embodiments, at least two, at least three, at least four, at least five, at least six, or all of the facilities may be co-located. As used herein, the term “co-located” refers to facilities in which at least a portion of the process streams and/or supporting equipment or services are shared between the two facilities. When two or more of the facilities shown in FIG. 1 are co-located, the facilities are within 40, within 35, within 30, within 20, within 15, within 12, within 10, within 8, within 5, within 2, or within 1 mile of one another, measured from their geographical center.

[0016] In one or more embodiments, all or a portion of the facility used to form the products as shown in FIG. 1 may be considered a chemical recycling facility, particularly the pyrolysis and cracking facilities. As used herein, the term “chemical recycling” refers to a recycling process that includes a step of chemically converting hydrocarbon waste materials into lower molecular weight molecules (e.g., polymers, oligomers, monomers, and/or non-polymeric molecules such as hydrogen and carbon monoxide) that are useful by themselves and/or are useful as feedstocks to another chemical production process or processes. A “chemical recycling facility,” is a facility for producing a recycle content product via chemical recycling of hydrocarbon waste, which can include, for example, waste plastic and biowaste. As used herein, the terms “recycle content” and “r-content” mean being or comprising a composition that is directly and/or indirectly derived from hydrocarbon waste, bio-naphtha, or combinations thereof.

[0017] Referring again to FIG. 1 , a feed stream comprising hydrocarbon waste material can be introduced into a pyrolysis facility. As used herein, the term “hydrocarbon waste” refers to used, scrap, and/or discarded material that is composed of at least 95 weight percent hydrocarbons. Examples of hydrocarbon waste material processed in facilities of the present technology can include, but are not limited to, waste plastic and biowaste. As used herein, the terms “waste plastic” and “plastic waste” can refer to used, scrap, and/or discarded plastic materials, such as plastic materials sent to a landfill or incinerator. As used herein, the term “biowaste” refers to material derived from living organisms or of organic origin. [0018] Turning now to FIG. 2, the feed locations of several types of feedstock suitable for use in the pyrolysis and cracking facilities according to one or more embodiments is provided.

[0019] As shown in FIG. 2, the hydrocarbon waste material introduced into the pyrolysis facility can include waste plastic, biowaste, and combinations thereof. In one or more embodiments, the combined feed to the pyrolysis unit can include at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.5 weight percent of waste plastic, based on the total weight of the hydrocarbon waste material. Alternatively, or in addition, the hydrocarbon waste material may comprise not more than 99, not more than 97, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 5, or not more than 2 weight percent of waste plastic, based on the total weight of the hydrocarbon waste material. The hydrocarbon waste material can include waste plastic in an amount of 10 to 99 weight percent, 15 to 95 weight percent, or 25 to 90 weight percent, based on the total weight of the hydrocarbon waste material in the feed stream, on a dry basis.

[0020] In one or more embodiments, the combined feed to the pyrolysis unit can include at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.5 weight percent of biowaste, based on the total weight of the hydrocarbon waste material. Alternatively, or in addition, the hydrocarbon waste material may comprise not more than 99, not more than 97, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 5, or not more than 2 weight percent of biowaste, based on the total weight of the hydrocarbon waste material. The hydrocarbon waste material introduced into the pyrolysis facility can comprise from 0.01 to 20, from 0.1 to 10, from 0.2 to 5, or from 0.5 to 1 weight percent of biowaste materials, based on the total weight of the hydrocarbon waste material, on a dry basis.

[0021] In one or more embodiments, a stream of bio-naphtha can also be introduced into at least one feed location within the cracking facility. As used herein, the term “bio-naphtha” refers to naphtha produced from renewable sources, usually by hydrotreatment of the renewable sources. Bio-naphtha comprises predominantly C8 to C24 paraffins, or C10 to C18 paraffins, and can originate from any suitable source of naturally occurring fats, oils, and fatty acids within the above carbon number range. Examples of suitable sources can include, but are not limited to, vegetable oils, waste food oils, byproducts of vegetable oil refining, oils such as palm, soybeans, rapeseed, sunflower, coconut, and corn, as well as animal and milk fats, and combinations thereof. Suitable bio-naphtha streams are described in, for example, U.S. Patent No. 8,648,224, which is incorporated herein by reference in its entirety to the extent not inconsistent with the present disclosure.

[0022] Turning now to FIG. 3, a diagram of the main steps/zones of a pyrolysis facility according to one or more embodiments of the present invention is provided. As used herein the term “pyrolysis” refers to the thermal decomposition of one or more organic materials at elevated temperatures in an inert (i.e., substantially oxygen free) atmosphere. A “pyrolysis facility” is a facility that includes all equipment, lines, and controls necessary to carry out pyrolysis of waste plastic and feedstocks derived therefrom.

[0023] FIG. 3 depicts an exemplary pyrolysis facility for converting a feed stream including, for example, hydrocarbon waste material, into a pyrolysis gas, a pyrolysis oil, and a pyrolysis residue. It should be understood that FIG. 3 depicts one exemplary embodiment of the present technology. Thus, certain features depicted in FIG. 3 may be omitted and/or additional features described elsewhere herein may be added to the system depicted in FIG. 3.

[0024] As shown in FIG. 3, a stream of hydrocarbon waste may be introduced into the pyrolysis reactor. As discussed previously with respect to FIG. 2, the hydrocarbon waste can include plastic waste, bio-waste, and combinations thereof. When the feed to the pyrolysis reactor includes both plastic waste and bio-waste, the two can be introduced into the pyrolysis reactor in the same stream or in separate streams. The combining of the two streams, when performed, may take place in a continuous or batch manner.

[0025] In general, and as depicted in FIG. 3, the pyrolysis facility can include a pyrolysis reactor and at least one separator for separating the product stream from the reactor. Although not depicted in FIG. 3, the separator can include various types of equipment including, but not limited to a filter system, a multistage separator, a condenser, and/or a quench tower. In an embodiment illustrated in FIG. 3, the pyrolysis facility can include both a solids separator for separating a stream of pyrolysis effluent from pyrolysis residue, and a gas separator for separating the pyrolysis oil from the pyrolysis gas.

[0026] In one or more embodiments, when the feed to the pyrolysis reactor includes oxygen-containing plastics (e.g., PET), the pyrolysis unit may include at least one hydrotreatment (e.g., hydrodeoxygenation) facility for removing oxygen from at least a portion of the pyrolysis effluent (e.g., pyrolysis gas, pyrolysis oil, or both).

[0027] In operation, at least a portion of the feed introduced into the pyrolysis reactor may be subjected to a pyrolysis reaction that produces a pyrolysis effluent comprising a pyrolysis oil, a pyrolysis gas, and a pyrolysis residue. As used herein, the term “pyrolysis gas” refers to a composition obtained from pyrolysis that is gaseous at 25°C at 1 atm. As used herein, the terms “pyrolysis oil” or “pyoil” refers to a composition obtained from pyrolysis that is liquid at 25°C and 1 atm. As used herein, the term “pyrolysis residue” refers to a composition obtained from pyrolysis that is not pyrolysis gas or pyrolysis oil and that comprises predominantly pyrolysis char and pyrolysis heavy waxes. As used herein, the term “pyrolysis char” refers to a carbon-containing composition obtained from pyrolysis that is solid at 200°C and 1 atm. As used herein, the term “pyrolysis heavy waxes,” refers to C20+ hydrocarbons obtained from pyrolysis that are not pyrolysis char, pyrolysis gas, or pyrolysis oil.

[0028] Pyrolysis is a process that involves the chemical and thermal decomposition of the introduced feed. Although all pyrolysis processes may be generally characterized by a reaction environment that is substantially free of oxygen, pyrolysis processes may be further defined, for example, by the pyrolysis reaction temperature within the reactor, the residence time in the pyrolysis reactor, the reactor type, the pressure within the pyrolysis reactor, and the presence or absence of pyrolysis catalysts.

[0029] The pyrolysis reactor can be any suitable type of reactor, including, but not limited to a film reactor, a screw extruder, a tubular reactor, a tank, a stirred tank reactor, a riser reactor, a fixed bed reactor, a fluidized bed reactor, a rotary kiln, a vacuum reactor, a microwave reactor, or an autoclave.

[0030] The temperature of the pyrolysis reactor can range from 325 to 1 ,100°C, 350 to 900°C, 350 to 700°C, 350 to 550°C, 350 to 475°C, 425 to 1 ,100°C, 425 to 800°C, 500 to 1 ,100°C, 500 to 800°C, 600 to 1 ,100°C, 600 to 800°C, 650 to 1 ,000°C, or 650 to 800°C.

[0031] The pressure within the pyrolysis reactor can be at least 0.1 , at least 0.2, or at least 0.3 bar and/or not more than 60, not more than 50, not more than 40, not more than 30, not more than 20, not more than 10, not more than 8, not more than 5, not more than 2, not more than 1.5, or not more than 1.1 bar. As used herein, the term “bar” refers to gauge pressure, unless otherwise noted.

[0032] The residence times of the feedstocks within the pyrolysis can range from 0.1 to 10 seconds, 0.5 to 10 seconds, 30 minutes to 4 hours, 30 minutes to 3 hours, or 1 hour to 3 hours, or 1 hour to 2 hours.

[0033] In some embodiments, the pyrolysis reaction can be performed in the presence of a catalyst, which may be introduced into the feed stream and/or directly into the reactor. The catalyst can be homogenous or heterogeneous and may include, for example, certain types of zeolites and other mesostructured catalysts. In some embodiments, the pyrolysis reaction may not be catalyzed (e.g., carried out in the absence of a pyrolysis catalyst), but may include a non-catalytic, heat-retaining inert additive, such as sand, in the reactor in order to facilitate heat transfer. Such catalyst-free pyrolysis processes may be referred to as “thermal pyrolysis.”

[0034] As shown in FIG. 3, the pyrolysis gas and pyrolysis oil may exit the solids separator as a pyrolysis vapor stream, which can subsequently be separated to form a stream of pyrolysis gas and pyrolysis oil. Subsequently, all or a portion of the pyrolysis gas can be liquified in a liquification zone, to form a liquified pyrolysis gas (LPyG). The gas separator and/or the liquification zone can include, for example, various coolers, vapor-liquid separators, and distillation columns (not shown in FIG. 3).

[0035] As shown in FIG. 3, the pyrolysis system described herein may produce a pyrolysis effluent that can be separated into a pyrolysis oil stream, a pyrolysis gas stream, and a pyrolysis residue stream, each of which may be directly used in various downstream applications based on their formulations. The various characteristics and properties of the pyrolysis oil, pyrolysis gas, and pyrolysis residue are described below. It should be noted that, while all of the following characteristics and properties may be listed separately, it is envisioned that each of the following characteristics and/or properties of the pyrolysis gas, pyrolysis oil, and/or pyrolysis residue are not mutually exclusive and may be combined and present in any combination.

[0036] In one or more embodiments, the pyrolysis oil may predominantly comprise hydrocarbons having from 4 to 30 carbon atoms per molecule (e.g., C4 to C30 hydrocarbons). As used herein, the term “Cx” or “Cx hydrocarbon,” refers to a hydrocarbon compound including “x” total carbons per molecule, and encompasses all olefins, paraffins, aromatics, heterocyclic, and isomers having that number of carbon atoms. For example, each of normal, iso, and t-butane, and all butenes and butadiene molecules would fall under the general description “C4.” The pyrolysis oil may have a C4-C30 hydrocarbon content of at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, or at least 95 weight percent based on the total weight of the pyrolysis oil stream. [0037] In one or more embodiments, the pyrolysis oil can predominantly comprise C5 to C25 hydrocarbons, C5 to C22 hydrocarbons, or C5 to C20 hydrocarbons. For example, the pyrolysis oil may comprise at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, or at least 95 weight percent of C5 to C25 hydrocarbons, C5 to C22 hydrocarbons, or C5 to C20 hydrocarbons, based on the total weight of the pyrolysis oil. The pyrolysis oil may have a C5-C12 hydrocarbon content of at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, or at least 55 weight percent based on the total weight of the pyrolysis oil. Additionally, or alternatively, the pyrolysis oil may have a C5-C12 hydrocarbon content of not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, or not more than 50 weight percent. The pyrolysis oil may have a C5-C12 hydrocarbon content in the range of 10 to 95 weight percent, 20 to 80 weight percent, or 35 to 80 weight percent, based on the total weight of the stream.

[0038] In one or more embodiments, the pyrolysis oil may also include various amounts of olefins and aromatics depending on reactor conditions and whether or not a catalyst is employed. The pyrolysis oil comprises at least 1 , at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, or at least 40 weight percent of olefins and/or aromatics based on the total weight of the pyrolysis oil. Additionally, or alternatively, the pyrolysis oil may include not more than 90, not more than 80, not more than 70, not more than 60, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 5, or not more than 1 weight percent of olefins and/or aromatics. As used herein, the term “aromatics” refers to the total amount (in weight) of any compounds containing an aromatic moiety, such as benzene, toluene, xylene, and styrene.

[0039] In one or more embodiments, the pyrolysis oil may have a paraffin (e.g., linear or branch alkanes) content of at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, or at least 65 weight percent based on the total weight of the pyrolysis oil. Additionally, or alternatively, the pyrolysis oil may have a paraffin content of not more than 99, not more than 97, not more than 95, not more than 93, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, or not more than 30 weight percent. The pyrolysis oil may have a paraffin content in the range of 25 to 90 weight percent, 35 to 90 weight percent, or 50 to 80 weight percent.

[0040] In one or more embodiments, the pyrolysis oil may have a mid-boiling point of at least 75°C, at least 80°C, at least 85°C, at least 90°C, at least 95°C, at least 100°C, at least 105°C, at least 110°C, or at least 115°C and/or not more than 250°C, not more than 245°C, not more than 240°C, not more than 235°C, not more than 230°C, not more than 225°C, not more than 220°C, not more than 215°C, not more than 210°C, not more than 205°C, not more than 200°C, not more than 195°C, not more than 190°C, not more than 185°C, not more than 180°C, not more than 175°C, not more than 170°C, not more than 165°C, not more than 160°C, not more than 155°C, not more than 150°C, not more than 145°C, not more than 140°C, not more than 135°C, not more than 130°C, not more than 125°C, or not more than 120°C, as measured according to ASTM D-5399. The pyrolysis oil may have a mid-boiling point in the range of 75 to 250°C, 90 to 225°C, or 115 to 190°C. As used herein, “mid-boiling point” refers to the median boiling point temperature of the pyrolysis oil, where 50 percent by volume of the pyrolysis oil boils above the mid-boiling point and 50 percent by volume boils below the mid-boiling point.

[0041] In one or more embodiments, the boiling point range of the pyrolysis oil may be such that at least 90 percent of the pyrolysis oil boils off at a temperature of 250°C, of 280°C, of 290°C, of 300°C, or of 310°C, as measured according to ASTM D-5399.

[0042] Turning to the pyrolysis gas, the pyrolysis gas can have a methane content of at least 1 , at least 2, at least 3, at least 4, at least 5, at least 6, at least 7, at least 8, at least 9, at least 10, at least 11 , at least 12, at least 13, at least 14, or at least 15 and/or not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, or not more than 20 weight percent based on the total weight of the pyrolysis gas. In an embodiment or in combination with any embodiment mentioned herein, the pyrolysis gas can have a methane content in the range of 1 to 50 weight percent, 5 to 50 weight percent, or 15 to 45 weight percent.

[0043] In one or more embodiments, the pyrolysis gas can have a C3 and/or C4 hydrocarbon content (including all hydrocarbons having 3 or 4 carbon atoms per molecule ) of at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, or at least 60 and/or not more than 99, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, or not more than 65 weight percent based on the total weight of the pyrolysis gas. The pyrolysis gas can have a C3 hydrocarbon content, a C4 hydrocarbon content, or combined C3 and C4 hydrocarbon content in the range of 10 to 90 weight percent, 25 to 90 weight percent, or 25 to 80 weight percent.

[0044] In one or more embodiments, the pyrolysis gas can make up at least 10, at least 20, at least 30, at least 40, or at least 50 weight percent of the total effluent from the pyrolysis reactor and the pyrolysis gas can have a combined ethylene and propylene content of at least 25, at least 40, at least 50, at least 60, at least 70, or at least 75 percent by total weight of the pyrolysis gas. [0045] Turning to the pyrolysis residue, in one or more embodiments, the pyrolysis residue comprises at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, or at least 85 weight percent of C20+ hydrocarbons based on the total weight of the pyrolysis residue. As used herein, “C20+ hydrocarbon” refers to hydrocarbon compounds containing at least 20 total carbons per molecule, and encompasses all olefins, paraffins, and isomers having that number of carbon atoms.

[0046] In an embodiment or in combination with any embodiment mentioned herein, the pyrolysis residue comprises at least 1 , at least 2, at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, or at least 99 weight percent of carbon-containing solids based on the total weight of the pyrolysis residue. Additionally, or alternatively, the pyrolysis residue comprises not more than 99, not more than 90, not more than 80, not more than 70, not more than 60, not more than 50, not more than 40, not more than 30, not more than 20, not more than 10, not more than 9, not more than 8, not more than 7, not more than 6, not more than 5, or not more than 4 weight percent of carbon-containing solids. As used herein, “carbon-containing solids” refer to carbon-containing compositions that are derived from pyrolysis and are solid at 25°C and 1 atm. The carbon-containing solids comprise at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 80, or at least 90 weight percent of carbon based on the total weight of the carbon-containing solids.

[0047] As shown in FIG. 3, in one or more embodiments, at least a portion of the pyrolysis gas may be cooled and at least partially condensed to form liquified pyrolysis gas (LPyG). Liquified pyrolysis gas can have a similar composition to the pyrolysis gas described herein. In some embodiments, the LPyG may include, for example, not more than 20, not more than 15, not more than 10, not more than 5, not more than 2, or not more than 1 weight percent of methane and lighter components, or components lighter than methane, based on the total weight of the stream. In some embodiments, the liquification zone includes a plurality of compressors, coolers, columns, and separators, to provide the final LPyG stream.

[0048] Turning now to FIG. 4, a diagram of the main steps/zones of a cracking facility are shown. As used herein, the term “cracking” refers to breaking down complex organic molecules into simpler molecules by the breaking of carbon-carbon bonds. A “cracking facility” is a facility that includes all equipment, lines, and controls necessary to carry out cracking of a feedstock derived from waste plastic. A cracking facility can include one or more cracker furnaces, as well as a downstream separation zone including equipment used to process the effluent of the cracker furnace(s). As used herein, the terms “cracker” and “cracking” are used interchangeably. [0049] FIG. 4 depicts an exemplary cracking facility for converting a cracker feed stream including, for example, pyrolysis effluent and/or bio-naphtha, into one or more recycle content hydrocarbon streams. It should be understood that FIG. 4 depicts one exemplary embodiment of the present technology. Thus, certain features depicted in FIG. 4 may be omitted and/or additional features described elsewhere herein may be added to the system depicted in FIG. 4.

[0050] As shown in FIG. 4, the cracker facility includes a cracker furnace, a pretreatment zone, and a separation zone. In general, cracked effluent from the furnace is subjected to various pretreatment steps (e.g., separation, compression, cooling, etc.) before being separated into various end products, including, for example, olefins, paraffins (at least a portion of which can be recycled to the furnace inlet as shown in FIG. 3), and other heavier hydrocarbon streams. When the feed to the cracker facility includes recycle content feed (e.g., bio-naphtha or a stream from the pyrolysis facility), the products from the cracker facility can be recycle content products.

[0051] As shown in FIG. 4, at least one pyrolysis fluid product or stream can be introduced into one or more feed locations within the cracker facility. As used herein, the term “pyrolysis fluid,” refers to a pyrolysis effluent stream that is in a fluid state (e.g., gas and/or liquid) at standard conditions of 25°C and 1 atm.

[0052] In one or more embodiments, the pyrolysis fluid stream can include at least one, at least two, at least three, or all of the following characteristics: (i) C9 hydrocarbons in an amount of from 5 to 99.5 weight percent, 10 to 95 weight percent, or 20 to 90 weight percent, based on the total weight of the stream; (ii) C5 to C12 weight percent hydrocarbons in an amount of from 25 to 99.5 weight percent, 40 to 99 weight percent, or 50 to 98 weight percent, based on the total weight of the stream; (iii) pentenes, CPD, and DCPD in a combined amount of at least 1 , at least 2, at least 5, at least 10, at least 15, at least 20, or at least 25 weight percent, based on the total weight of the stream; and (iv) comprises less than 25, less than 10, less than 5, less than 2, or less than 1 weight percent of non-hydrocarbon components. Where multiple pyrolysis fluid streams are introduced into a single cracking facility, the properties describe the stream introduced into a single feed location and streams introduced into other feed locations may have the same or different properties. The pyrolysis fluid stream can also have one or more properties in the above-discussed ranges.

[0053] In one or more embodiments, the pyrolysis fluid stream can include at least one, at least two, or all of the following characteristics: (i) C5-C12 hydrocarbons in an amount of 25-99.5 weight percent, 0-99 weight percent, 50- 98 weight percent; (ii) pentenes, CPD, and DCPD in a combined amount of at least 1 , at least 2, at least 5, at least 10, at least 15, at least 20, at least 25 weight percent; and/or (iii) less than 25, less than 10, less than 5, less than 2, or less than 1 weight percent of non-hydrocarbon components, wherein all weight percentages are based on the total weight of the pyrolysis stream. Where multiple pyrolysis fluid streams are introduced into a single cracking facility, the properties describe the stream introduced into a single feed location and streams introduced into other feed locations may have the same or different properties.

[0054] As shown in FIG. 4, in some embodiments, a pyrolysis oil stream may be introduced into at least one feed location upstream of the cracker furnace, while a pyrolysis gas stream can be introduced into a feed location upstream or downstream of the furnace. For example, a stream comprising pyrolysis oil can be introduced into the cracker furnace inlet, while a pyrolysis gas containing stream may be introduced to a location downstream of the outlet of the furnace. When introduced downstream of the furnace, the pyrolysis gas can be combined with at least a portion of the olefin-containing effluent stream exiting the furnace outlet. Examples of feed locations downstream of the furnace outlet include a feed location feed locations within the pretreatment zone (such as, for example, upstream of one or more compression stages), a feed location upstream of the separation zone, and feed locations upstream of one or more columns within the separation zone (not shown in FIG. 4). When multiple streams of pyrolysis gas and/or pyrolysis oil are introduced into the cracker facility, the streams can originate from the same or different pyrolysis or other sources (facilities, entities, etc.) The introduction of the pyrolysis fluid stream into the cracking facility can be performed continuously or in a batchwise manner.

[0055] Depending on where the pyrolysis fluid (pyrolysis oil and/or pyrolysis gas) is introduced into the cracking facility, the stream may be further heated, cooled, condensed, and/or compressed prior to combination with the corresponding cracker stream or zone. When combined with a stream or introduced into a zone within the cracking facility, the temperature of the pyrolysis fluid can be within 50, within 40, within 30, or within 20°C of the cracker stream or zone with which it is combined, while the pressure of the pyrolysis fluid stream can be within about 100, within 75, or within 50 psi of the cracker stream or zone. In general, the temperature and/or pressure of the pyrolysis fluid can be within 25, within 20, within 15, within 10, or within 5 percent of the temperature and/or pressure of the cracker stream or zone with which it is combined.

[0056] As shown in FIG. 4, a stream of pyrolysis gas and/or pyrolysis oil may be introduced into the cracker facility along with or as the cracker feed stream. In some embodiments, the cracker feed stream can comprise at least 1 , at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, or at least 95 weight percent of pyrolysis gas, pyrolysis oil, or pyrolysis gas and pyrolysis oil combined, based on the total weight of the stream. Alternatively, or in addition, the cracker feed stream can comprise not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, or not more than 20 weight percent of pyrolysis gas, pyrolysis oil, or a combination of pyrolysis gas and pyrolysis oil, based on the total weight of the stream, or it can include these components in an amount in the range of from 1 to 95 weight percent, 5 to 90 weight percent, or 10 to 85 percent, based on the total weight of the stream. [0057] Alternatively, or in addition, the feed to the cracker facility can include bio-naphtha. When present, the cracker feed stream can comprise at least 1 , at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, or at least 95 weight percent of bio-naphtha, based on the total weight of the stream. Alternatively, or in addition, the cracker feed stream can comprise not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, or not more than 20 weight percent of bio-naphtha, based on the total weight of the stream, or it can include bio-naphtha in an amount in the range of from 1 to 95 weight percent, 5 to 90 weight percent, or 10 to 85 percent, based on the total weight of the stream.

[0058] In some embodiments, the cracker feed stream can include at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, or at least 95 weight percent and/or not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, or not more than 20 weight percent of a hydrocarbon feed other than pyrolysis gas, pyrolysis oil, and bio-naphtha based on the total weight of the cracker feed stream. The pyrolysis gas can be in a vapor state, or can be liquified pyrolysis gas, or a combination. In some embodiments, a pyrolysis fluid may be introduced at only one of the feed locations shown in FIG. 4, while, in other embodiments, pyrolysis fluid may be introduced into two or more of these feed locations.

[0059] Regardless of the source of the stream, in some embodiments, the cracker feed may comprise a predominantly C2 to C4 hydrocarbon containing composition. As used herein, the term “predominantly C2 to C4 hydrocarbon,” refers to a stream or composition containing at least 50 weight percent of C2 to C4 hydrocarbon components. Examples of specific types of C2 to C4 hydrocarbon streams or compositions include propane, ethane, butane, and LPG. The cracker feed stream may comprise at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, in each case wt.% based on the total weight of the feed, and/or not more than 100, or not more than 99, or not more than 95, or not more than 92, or not more than 90, or not more than 85, or not more than 80, or not more than 75, or not more than 70, or not more than 65, or not more than 60, in each case weight percent C2 to C4 hydrocarbons or linear alkanes, based on the total weight of the feed. The cracker feed stream can comprise predominantly propane, predominantly ethane, predominantly butane, or a combination of two or more of these components.

[0060] In some embodiments, the cracker feed can comprise a predominantly C5 to C22 hydrocarbon containing composition. As used herein, “predominantly C5 to C22 hydrocarbon” refers to a stream or composition comprising at least 50 weight percent of C5 to C22 hydrocarbon components. Examples of C5 to C22 range streams include gasoline, naphtha, middle distillates, diesel, kerosene.

[0061] In one or more embodiments, the cracker feed stream may comprise at least 20, or at least 25, or at least 30, or at least 35, or at least 40, or at least 45, or at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, in each case wt.% and/or not more than 100, or not more than 99, or not more than 95, or not more than 92, or not more than 90, or not more than 85, or not more than 80, or not more than 75, or not more than 70, or not more than 65, or not more than 60, in each case weight percent C5 to C22, or C5 to C20 hydrocarbons, based on the total weight of the stream, or it can include C5 to C22 in an amount in the range of from 20 to 100 weight percent, 25 to 95 weight percent, or 30 to 85 weight percent, based on the total weight of the stream.

[0062] In some embodiments, the cracker feed may have a C15 and heavier (C15+) content of at least 0.5, or at least 1 , or at least 2, or at least 5, in each case weight percent and/or not more than 40, or not more than 35, or not more than 30, or not more than 25, or not more than 20, or not more than 18, or not more than 15, or not more than 12, or not more than 10, or not more than 5, or not more than 3, in each case weight percent, based on the total weight of the feed, or it can be in the range of from 0.5 to 40 weight percent, 1 to 35 weight percent, or 2 to 30 weight percent, based on the total weight of the stream. [0063] In some embodiments, the cracker feed can comprise vacuum gas oil (VGO), hydrogenated vacuum gas oil (HVGO), or atmospheric gas oil (AGO). The cracker feed stream can comprise at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, or at least 90 and/or not more than 99, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, or not more than 50 weight percent of at least one gas oil, based on the total weight of the stream, or it can be present in an amount in the range of from 5 to 99 weight percent, 10 to 90 weight percent, or 15 to 85 weight percent, or 5 to 50 weight percent, based on the total weight of the stream.

[0064] Turning now to FIG. 5, a more detailed diagram of the main steps of a cracker facility similar to that depicted in FIG. 4 are shown.

[0065] As shown in FIG. 5, the cracker feed is introduced into a cracking furnace, wherein the hydrocarbon components therein are thermally cracked to form lighter hydrocarbons, including olefins such as ethylene, propylene, and/or butadiene, as well as benzene, toluene, xylene (BTX) and C9 and heavier hydrocarbon components. The residence time of the cracker stream the furnace can be in the range of from 0.15 to 2 seconds, 0.20 to 1.75 seconds, or 0.25 to 1 .5 seconds. The temperature of the furnace (typically measured as the temperature of the cracked olefin-containing effluent stream withdrawn from the furnace outlet) can be in the range of from 730 to 900°C, 750 to 875°C, or 750 to 850°C.

[0066] The furnace can be any suitable type of furnace for cracking the feed stream. In some embodiments, the cracking furnace can be a liquid or naphtha cracker receiving a cracker feed stream containing at least 50 wt.%, or at least 75 wt.%, or at least 85 wt.% liquid (when measured at 25°C and 1 atm) hydrocarbons having a carbon number from C5-C22. In some embodiments, the cracker feed stream can be cracked in a gas furnace. A gas furnace is a furnace having at least one coil which receives (or operated to receive or configured to receive), at the inlet of the coil at the entrance to the convection zone, a predominately vapor-phase feed (more than 50% of the weight of the feed is vapor) (“gas coil”). The gas coil can receive a predominately C2-C4 feedstock, or a predominately a C2-C3 feedstock, to the inlet of the coil in the convection section, or alternatively, having at least one coil receiving more than 50 wt.% ethane and/or more than 50% propane and/or more than 50% LPG, or in any one of these cases at least 60 wt.%, or at least 70 wt.%, or at least 80 wt.%, based on the weight of the cracker feed to the coil, or alternatively based on the weight of the cracker feed to the convection zone.

[0067] The furnace can be a thermal gas cracker and can, in some embodiments, be a thermal steam gas cracker in the presence of steam. Steam cracking refers to the high-temperature cracking (decomposition) of hydrocarbons in the presence of steam.

[0068] The stream withdrawn from the furnace outlet can comprise a stream of olefins and other hydrocarbons lighter than the cracker feed. This olefin- containing effluent stream can comprise at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, or at least 90 weight percent of C2 to C4 olefins.

[0069] As shown in FIG. 6, the furnace effluent may be introduced into a fractionation/quenching zone, wherein the stream can be cooled and at least partially condensed. In some embodiments, the olefin-containing effluent may be cooled using a liquid quench stream in a quench tower, while, in other embodiments, the cooling may be at least partially carried out with a heat exchanger (e.g., a transfer line heat exchanger, or TLE). As a result of the cooling and separation, one or more streams enriched in heavier hydrocarbon components (e.g., C5 and heavier) can be withdrawn from the fractionation/quenching zone, while a stream enriched in lighter hydrocarbon components (e.g., C4 and lighter) can be introduced into a downstream compressor zone.

[0070] In the compressor zone, the pressure of the lighter hydrocarbon vapor stream may be increased via passage through a multi-stage compressor having, for example, 2 to 10 stages, 3 to 8 stages, or 4 to 7 stages. The compression zone can include interim cooling and knock-out of heavy components, according to conventional compression trains. The compressed, treated stream can be introduced into a separation zone, wherein it can be separated into two or more hydrocarbon product streams via passage through one or more fractionation columns in the separation zone of the cracking facility, as generally shown in FIG. 5.

[0071] As used herein, the term “fractionation” refers to the general process of separating two or more materials having different boiling points. Examples of equipment and processes that utilize fractionation include, but are not limited to, distillation, rectification, stripping, and vapor-liquid separation (single stage). [0072] In one or more embodiments, the fractionation section of the cracker facility may include one or more of a demethanizer, a deethanizer, a depropanizer, an ethylene splitter, a propylene splitter, a debutanizer, and combinations thereof. As used herein, the term “demethanizer,” refers to a column whose light key component is methane. Similarly, “deethanizer,” and “depropanizer,” refer to columns with ethane and propane as the light key component, respectively. A “splitter” column separates an olefin from a paraffin of the same carbon number (and heavier components). Thus, an “ethylene splitter” removes ethylene as the light key from ethane and heavier components and a “propylene splitter” removes propylene as the light key from propane and heavier components.

[0073] Any suitable arrangement of columns may be used so that the fractionation section provides at least one olefin product stream, at least one paraffin stream, and at least one pyrolysis gasoline stream suitable for producing hydrocarbon resin. As used herein, the term “pyrolysis gasoline” refers to a composition including mainly C4 to C12 hydrocarbons and having boiling point range of from 30°C to 250°C formed in a cracking facility. The pyrolysis gasoline may or may not comprise or originate from a pyrolysis fluid. As shown in FIG. 5, the pyrolysis gasoline can include one or more of a heavy condensate stream from the quench/fractionation zone, a light hydrocarbon condensate stream from the compressor zone, and at least one overhead or bottoms stream (e.g., debutanizer bottoms stream) from the separation zone of the cracker facility.

[0074] One exemplary arrangement of a fractionation section of the separation zone is shown in FIG. 5. According to this configuration of the fractionation section, the pressurized stream from the compressor zone can pass through a demethanizer column, wherein the methane and lighter (CO, CO2, H2) components are separated from the ethane and heavier components. The demethanizer can be operated at a temperature of from -145 to -120°C, - 140 to -125°C, or -135 to -130°C. The bottoms stream from the demethanizer column includes at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95 or at least 99 of ethane and heavier components, based on the total weight of the stream.

[0075] At least a portion of the stream introduced into the fractionation section (e.g., all or a portion of the demethanizer bottoms stream as shown in FIG. 5) can be introduced into a deethanizer column, wherein the C2 and lighter components can be separated from the C3 and heavier components by fractional distillation. The deethanizer can be operated with an overhead temperature of -35 to -5°C, -30 to -10°C, or -20 to -15°C and an overhead pressure of 3 to 20 barg, 7 to 15 barg, or 8 to 15 barg. The overhead stream removed from the deethanizer column comprises at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, in each case weight percent of ethane and ethylene, based on the total weight of the overhead stream.

[0076] In some embodiments, the C2 and lighter overhead stream from the deethanizer can be further separated in an ethylene splitter. In the ethylene splitter, an ethylene and lighter component stream can be withdrawn from the overhead of the column or as a side stream from the top half of the column, while the ethane and any residual heavier components are removed in the bottoms stream. The ethylene fractionator may be operated at an overhead temperature of -45 to -15°C, -40 to -20°C, or -30 to -20°C and an overhead pressure of 10 to 25 barg, 12 to 22 barg, or 15 to 20 barg. The overhead stream, which may be enriched in ethylene, can include at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, or at least 97, or at least 98, or at least 99, in each case weight percent ethylene, based on the total weight of the stream.

[0077] The bottoms stream from the ethylene splitter may include at least 40, or at least 45, or at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, or at least 98, in each case weight percent ethane, based on the total weight of the bottoms stream. All or a portion of the recovered ethane may be recycled to the inlet of the cracker furnace as additional feedstock, alone or in combination with the pyrolysis oil, pyrolysis gas, and/or bio-naphtha as discussed previously.

[0078] In some embodiments, at least a portion of the compressed stream fed to the separation zone may be introduced into a depropanizer (e.g., the deethanizer bottoms stream as shown in FIG. 5), wherein C3 and lighter components are removed as an overhead vapor stream, while C4 and heavier components exit the column in the liquid bottoms. The depropanizer can be operated with an overhead temperature of 20 to 70°C, 35 to 65°C, or 40 to 60°C and an overhead pressure of 10 to 20 barg or 12 to 17 barg. The overhead stream removed from the depropanizer column can comprise at least or at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, or at least 98, in each case weight percent of propane and propylene, based on the total weight of the overhead stream.

[0079] In some embodiments, the overhead stream from the depropanizer may be introduced into a propylene splitter, wherein the propylene and any lighter components are removed in the overhead stream and the propane and any heavier components exit the column in the bottoms stream. The propylene fractionator may be operated at an overhead temperature of 20 to 55°C, 25 to 50°C, or 30 to 45°C and an overhead pressure of 12 to 20 barg or 15 to 17 barg. The overhead stream can include at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, or at least 97, or at least 98, or at least 99, in each case weight percent propylene, based on the total weight of the stream and may be sent to downstream processing unit for further processing, storage, or sale.

[0080] The bottoms stream from the propylene splitter may include at least 40, or at least 45, or at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, or at least 98, in each case weight percent propane, based on the total weight of the bottoms stream. All or a portion of the recovered propane may be recycled to the cracker furnace as additional feedstock, alone or in combination with pyrolysis oil, pyrolysis gas, and/or bio-naphtha as discussed previously.

[0081] In one or more embodiments, at least a portion of the compressed stream (e.g., the bottoms stream from the depropanizer as shown in FIG. 5) may be sent to a debutanizer column for separating C4 and lighter components, including butenes, butanes and butadienes, from C5 and heavier (C5+) components. The debutanizer can be operated with an overhead temperature of 20 to 70°C, 25 to 65°C, or 30 to 60°C and an overhead pressure of 2 to 8 barg or 3 to 6 barg.

[0082] In one or more embodiments, the overhead stream removed from the debutanizer column comprises at least 30, or at least 35, or at least 40, or at least 45, or at least 50, or at least 55, or at least 60, or at least 65, or at least 70, or at least 75, or at least 80, or at least 85, or at least 90, or at least 95, in each case weight percent of butadiene, based on the total weight of the stream. The bottoms stream from the debutanizer, which may be a light pyrolysis gasoline stream, includes mainly C5 and heavier components, in an amount of at least 50, or at least 60, or at least 70, or at least 80, or at least 90, or at least 95 weight percent, based on the total weight of the stream. [0083] In one or more embodiments, the light pyrolysis gasoline stream (e.g., debutanizer bottoms) can have a boiling range in the range of from 20 to 100°C, 25 to 95°C, or 30 to 80°C, and can include mainly C5 to C12 hydrocarbon components, such that the total amount of C5 to C12 hydrocarbon components in the light pyrolysis gasoline stream can be at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.9 weight percent, based on the total weight of the stream. The light pyrolysis gasoline can also include 2 to 30 weight percent, 5 to 25 weight percent, or 8 to 20 weight percent of C5 and lighter components (including olefins and diolefins), and C6 to C8 components in an amount from 5 to 60 weight percent, 10 to 55 weight percent, or 25 to 50 weight percent, based on the total weight of the stream. The combined amount of CPD, DCPD, and pentenes in the light pyrolysis gasoline stream can be in the range of from 5 to 50 weight percent, 10 to 45 weight percent, or 15 to 40 weight percent, based on the total weight of the stream. [0084] The light pyrolysis gasoline stream withdrawn from the bottom of the debutanizer can also have a Gardner color of 1 to 8 or 2 to 5, and a sulfur content of 50 to 300 ppm by weight or 100 to 250 ppm by weight. The density of this stream can be from 0.60 to 1.00 g/ml, 0.65 to 0.95 g/ml or 0.75 to 0.90 g/ml.

[0085] As shown in FIG. 5, the debutanizer bottoms stream withdrawn from the separation zone in the cracker facility may optionally be combined with one or more heavier pyrolysis gasoline streams (also called hydrocarbon condensate streams) from one or more upstream zones of the cracker facility. For example, the light pyrolysis gasoline may be combined with a stream of heavy hydrocarbon condensate from the fractionation/quench section of the facility, and/or with a stream of light hydrocarbon condensate from the compressor section. Additional details about exemplary compositions of these streams are provided below.

[0086] In one or more embodiments, the heavy hydrocarbon condensate stream withdrawn from the fractionation/quench zone may have a boiling range in the range of from 150 to 300°C, 160 to 275°C, or 180 to 250°C, and can include mainly C9 and heavier components, such that the total amount of C9 and heavier components (or C10 and heavier components) in the heavy hydrocarbon condensate stream can be at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.9 weight percent, based on the total weight of the stream. The heavy hydrocarbon condensate stream can also have a Gardner color of 2 to 12 or 2 to 11 , and a sulfur content of 200 to 1000 ppm by weight or 300 to 800 ppm by weight. The density of this stream can be from 0.90 to 1 .15 g/ml, 0.92 to 1.10 g/ml or 0.95 to 1 .05 g/ml. [0087] In one or more embodiments, the heavy hydrocarbon condensate stream can have a boiling point range of from 70 to 275°C, 75 to 250°C, or 80 to 240°C, and a total amount of C8 and lighter components in the range of from 2 to 25 weight percent or 5 to 20 weight percent, based on the total weight of the stream. The heavy hydrocarbon condensate stream can comprise mainly C8 and C9 components, with the total amount of C8 and C9s in the range of from 20 to 80 weight percent, 25 to 75 weight percent, or 30 to 70 weight percent, based on the total weight of the stream. The amount of C10 and heavier components in this stream can be not more than 50, not more than 45, or not more than 40 weight percent, based on the total weight of the stream. The Gardner color can be from 2 to 10 or 3 to 8 and the sulfur content can be from 100 to 600 ppm or 250 to 450 ppm. The heavy hydrocarbon condensate stream density can be between 0.85 and 1 .05 g/ml or 0.90 to 0.95 g/ml.

[0088] In some embodiments, the debutanizer bottoms stream (and/or the heavy hydrocarbon condensate stream from the fractionation/quench zone) may also be combined with a light hydrocarbon condensate stream withdrawn from the compressor zone. In some embodiments, this light hydrocarbon condensate stream may be a heavy pyrolysis gasoline stream. The light hydrocarbon condensate stream from the compressor may have a boiling point range of 35 to 125°C, 40 to 115°C, or 50 to 100°C, and can include C6 and lighter hydrocarbons in an amount of at least 45, at least 50, at least 55, or at least 60 weight percent, based on the total weight of the stream. The total amount of C9 and heavier components in this stream can be not more than 25, not more than 20, not more than 17, not more than 15, not more than 12, or not more than 10 weight percent, based on the total weight of the stream. The Gardner color of this stream can be from 2 to 8 or 3 to 6 and the sulfur content can be from 50 to 300 ppm or 100 to 250 ppm. The density of the light hydrocarbon condensate stream can be 0.65 to 1.0 g/ml, 0.75 to 0.95 g/ml, or 0.85 to 0.90 g/ml.

[0089] In one or more embodiments, all or a portion of the pyrolysis gasoline withdrawn from the cracking facility (which can include, for example, the heavy hydrocarbon condensate, the light hydrocarbon condensate, and/or the debutanizer column bottoms) can be passed through a treatment step/zone to separate out (or concentrate) one or more less desired components to thereby form a feed stream for the downstream hydrocarbon resin production facility. [0090] For example, when the resin being produced in the hydrocarbon resin production facility is a C9 resin (as discussed in further detail below), the treatment step/zone shown in FIG. 5 can include concentration of C8 to C10 reactable monomers (e.g., olefins, diolefins, and cyclic olefins) via one or more distillation steps. For example, the pyrolysis gasoline stream may be passed through one or more columns to remove C8 inerts and C7 and lighter components, and another one or more columns to remove C10 inerts and C11 and heavier components. The resulting hydrocarbon stream, which can be a recycle content hydrocarbon stream, can include C8 to C10 polymerizable monomers (or aromatics) in an amount of at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, or at least 97 weight percent, based on the total weight of the stream. The lighter and heavier components removed from the pyrolysis gasoline stream may be further used, processed, and/or sold.

[0091] Turning now to FIG. 6, an example of one integrated configuration of a pyrolysis facility and a cracking facility is shown.

[0092] In the embodiment illustrated in FIG. 6, hydrocarbon waste material introduced into the pyrolysis facility can be pyrolyzed to form a pyrolysis fluid (and, in particular, a pyrolysis gas), and all or a portion of it can be quenched within the cracking facility, as generally shown in FIG. 4. Alternatively, in one or more embodiments, a separate quench zone can be used, and the cooled stream from this separate quench zone can be introduced into the fractionation zone of the cracking facility along with the cooled stream from the quench zone of the cracking facility. In some cases, the pyrolysis gas can be in vapor state when introduced into the quench zone, while, in other cases, it can be a liquified pyrolysis gas as discussed previously.

[0093] Referring again to FIG. 1 , an effluent stream from the cracking facility including at least one hydrocarbon resin monomer can optionally be passed through a treatment step/zone prior to being introduced into the hydrocarbon resin production facility. Such a treatment facility can be configured to remove impurities (such as sulfur), or can be configured to remove one or more components which are not desired in the final hydrocarbon resin composition. For example, in some embodiments, the treatment facility can be used to remove C7 and lighter components and C10 inert and heavier components. In other embodiments, the treatment facility is not used, and all or a portion of the pyrolysis gas stream may be withdrawn from the cracking facility.

[0094] As shown in FIG. 1 , whether treated or not, the hydrocarbon stream may be introduced into a hydrocarbon resin production facility, wherein it may be converted or formed into a hydrocarbon resin. “Flydrocarbon resin” when used herein means a thermoplastic resin, or starting thermoplastic resins, having a number average molecular weight of less than 5,000 g/mol as measured by GPC. Flydrocarbon resins include aromatic-modified, hydrogenated, partially-hydrogenated, and non-hydrogenated versions of these resins.

[0095] In one embodiment, the hydrocarbon resin produced may be a C9 hydrocarbon resin. The terms “C9 thermoplastic resin” and “C9 hydrocarbon resin” as used herein means an aromatic C9 hydrocarbon thermoplastic resin that is a thermoplastic resin produced from the polymerization of monomers comprising unsaturated aromatic C8, C9, and/or C10 species boiling in the range from about 100°C to about 300°C at atmospheric pressure. These monomers are typically generated from petroleum processing, e.g. cracking, with or without refining crude streams to highly purified monomer species. The aromatic C9 hydrocarbon thermoplastic resins of this invention can be produced by any method known in the art. Aromatic C9 hydrocarbon thermoplastic resins are in one embodiment prepared by cationic polymerization of aromatic C8, C9, and/or C10 unsaturated monomers derived from petroleum distillates resulting from naphtha cracking and are referred to as “C9 monomers.”

[0096] These monomer streams are comprised of cationically polymerizable monomers such as styrene, alpha methyl styrene (AMS), beta-methyl styrene, vinyl toluene, indene, dicyclopentadiene, divinylbenzene, and other alkyl substituted derivatives of these components. Aliphatic olefin monomers with four to six carbon atoms are also present during polymerization in some embodiments of C9 resins. The polymerization is in some instances catalyzed using Friedel-Crafts polymerization catalysts such as Lewis acids (e.g., boron trifluoride (BF3), complexes of boron trifluoride, aluminum trichloride (AICI3), and alkyl aluminum chlorides). In other instances, the polymerization used to form the C9 resin can be or comprise thermal polymerization. In addition to the reactive components, nonpolymerizable components include, but are not limited to, aromatic hydrocarbons such as xylene, ethyl benzene, cumene, ethyl toluene, indane, methylindane, naphthalene, and other similar chemical species. The nonpolymerizable components of the feed stream are in some embodiments incorporated into the thermoplastic resins via alkylation reactions. C9 hydrocarbon thermoplastic resins include non-hydrogenated, partially hydrogenated, or fully hydrogenated resins. Aromatic C9 hydrocarbon thermoplastic resins can be obtained as Picco® C9 thermoplastic resin, and aliphatic hydrogenated and aliphatic/aromatic partially hydrogenated C9 H2 hydrocarbon thermoplastic resins can be obtained as Regalite® thermoplastic resin from Eastman Chemical Company.

[0097] It is to be understood that encompassed by the above definition are hydrogenated, partially hydrogenated, and non-hydrogenated versions of these resins, that these thermoplastic resins include resins of similar types generated by mixing or blending of dissimilar feedstocks to produce heterogeneous mixtures of the feedstocks used to generate the thermoplastic resins. [0098] Turning now to FIG. 7, a diagram of the main steps of a resin production facility according to one or more embodiments of the present technology is provided.

[0099] FIG. 7 depicts an exemplary C9 resin production facility for converting a hydrocarbon feed stream into a C9 hydrocarbon resin. It should be understood that FIG. 7 depicts one exemplary embodiment of the present technology. Thus, certain features depicted in FIG. 7 may be omitted and/or additional features described elsewhere herein may be added to the system depicted in FIG. 7.

[00100] As shown in FIG. 7, a hydrocarbon feed stream (e.g., a pyrolysis gas stream), which can be a recycle content hydrocarbon feed stream (e.g., a recycle content pyrolysis gas), can be introduced into a preliminary feed treatment zone of the hydrocarbon resin production facility. In the feed treatment zone, the feed stream can be pretreated in one or more of a number of different processing steps, including, but not limited to various separation steps, such as optionally removing select components from the feed stream, and/or molecular weight adjustment steps. For example, in some embodiments, the feed treatment zone can include a section or step of cracking heavier components (e.g., dicyclopentadiene) to lighter components (e.g., cyclopentadiene) and then separating out the lighter components prior to entering the polymerization zone. The specific steps in the pretreatment zone depend, at least in part, on the feed stream composition and the final resin product being produced.

[00101] In one or more embodiments, the hydrocarbon feed stream introduced into the hydrocarbon resin facility can comprise predominantly C9 hydrocarbon components. For example, it can include at least 10, at least 25, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, or at least 95 and/or not more than 99.9, not more than 99.5, not more than 99, not more than 97, not more than 95, not more than 90, not more than 85, or not more than 80 weight percent of C9 hydrocarbons, based on the total weight of the stream, or it can include C9 hydrocarbons in an amount of 10 to 95 weight percent, 20 to 90 weight percent, or 25 to 50 weight percent, based on the total weight of the stream.

[00102] The hydrocarbon feed stream to the C9 hydrocarbon resin production facility can include C7 to C12 hydrocarbons in a combined amount in the range of 40 to 99 weight percent, 50 to 98 weight percent, or 75 to 95 weight percent, based on the total weight of the stream. The stream can also include BTX (benzene, toluene, xylene) in a combined amount in the range of from 1 to 50 weight percent, 5 to 30 weight percent, or 10 to 25 weight percent, based on the total weight of the stream.

[00103] The boiling point range of the hydrocarbon feed stream introduced into the C9 hydrocarbon resin production facility can be 30 to 350°C, 50 to 300°C, or 80 to 250°C. The stream can have a mid-boiling temperature of 100 to 250°C, 125 to 200°C, or 140 to 180°C, and a 10% boiling temperature of 50 to 150°C, 75 to 125°C, or 80 to 110°C. The hydrocarbon feed stream (which can be a recycle content hydrocarbon feed stream) fed to the C9 hydrocarbon resin production facility can have a 90% boiling temperature of 120°C to 260°C, 150 to 250°C, or 180 to 240°C.

[00104] The specific gravity of the hydrocarbon feed stream introduced into the C9 hydrocarbon resin production facility can be at least 0.60, at least 0.65, at least 0.70, or at least 0.73 and/or not more than 0.95, not more than 0.92, or not more than 0.90, measured at 60°F.

[00105] The hydrocarbon feed stream introduced into the C9 hydrocarbon resin production facility can have a Gardner color of not more than 12, not more than 10, not more than 8, not more than 6, not more than 4, not more than 3, not more than 2, or not more than 1 , and the sulfur content of the stream can be at least 5, at least 7, or at least 10 ppm and/or not more than 500, not more than 400, or not more than 300, not more than 200, or not more than 100 ppm, based on the total weight of the stream.

[00106] The hydrocarbon feed stream introduced into the C9 hydrocarbon resin production facility can include lights (C2 to C4 components) in an amount of 0.1 to 2 weight percent, 0.15 to 1.75 weight percent, or 0.2 to 1.5 weight percent, based on the total weight of the stream. The hydrocarbon feed stream introduced into the C9 hydrocarbon resin production facility can include benzene in an amount of not more than 70, not more than 65, not more than 60, not more than 55, not more than 50 weight percent, based on the total weight of the stream.

[00107] The hydrocarbon feed stream introduced into the C9 hydrocarbon resin production facility can wherein the recycle content hydrocarbon stream exhibits at least one, at least two, at least three, at least four, at least five, at least six, or all seven of the following characteristics: (i) a boiling range within 30-350°C, 50-300°C, 80-250°C; (ii) a mid-boiling temperature of 100-250°C, 125-200°C, 140-180°C; (iii) a 10% boiling temperature in the range of 50- 150°C, 75-125°C, 80-110°C; (iv) a 90% boiling temperature in the range of 120- 260°C, 150-250°C, 180-240°C; (v) C7-C12 hydrocarbons in a combined amount of 40-99 weight percent, 50-98 weight percent, 75-95 weight percent; (vi) C9 hydrocarbons in a combined amount of 10-95 weight percent, 20-90 weight percent, 25-50 weight percent, and (vii) BTX in a combined amount of 1 -50 weight percent, 5-30 weight percent, 10-25 weight percent, wherein each weight percent is based on the total weight of the hydrocarbon feed stream. [00108] The hydrocarbon stream fed to the C9 resin facility can be a recycle content hydrocarbon stream. It may have a recycle content of at least 1 , at least 2, at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.5 weight percent and/or not more than 99, not more than 97, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 5, or not more than 2 weight percent.

[00109] When the hydrocarbon feed stream is a recycle content hydrocarbon feed stream, all or a portion of the stream may originate from an upstream cracking or pyrolysis facility. In one or more embodiments, the recycle content hydrocarbon stream introduced into the C9 hydrocarbon resin production facility can include components from one or more of the following streams: (i) a hydrocarbon condensate stream withdrawn from the fuel oil fractionation/quench section of a cracking facility (e.g., a heavy hydrocarbon condensate); (ii) a pyrolysis gasoline (e.g., light hydrocarbon condensate) stream withdrawn from the compressor section of a cracker facility, and/or (iii) a light pyrolysis gasoline stream withdrawn from the separation section of a cracker facility (such as, for example, the bottoms stream withdrawn from the debutanizer). When more than one of these streams are utilized, they can originate from the same or from different upstream cracking facilities.

[00110] As shown in FIG. 7, at least a portion of the recycle content hydrocarbon stream (e.g., the r-pyrolysis gasoline from the cracker facility) can be introduced into a distillation zone, wherein the light ends (e.g., C7 and lighter) and heavy ends (C10 inerts and heavier) can be removed from the stream. The resulting stream can include at least about 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 92, at least 95, at least 97, or at least 99 weight percent of C8 to C10 aromatics, based on the total weight of the stream. Examples of such compounds can include, but are not limited to, xylene, styrene, alpha methylstyrene, dicyclopentadiene (DCPD), vinyl toluenes, indene, methylindene, and combinations thereof. This stream can include 50-100, 55- 99, or 60-95 weight percent of aromatic monomers, based on the total weight of the stream. The balance of the stream can comprise C4 to C12 non-aromatic monomers.

[00111] As shown in FIG. 7, the treated stream from the feed treatment zone can be introduced into a polymer formation or polymerization zone. As shown in FIG. 7, the treated stream can then be passed to a polymerization zone, wherein the feed is polymerized to form a crude C9 hydrocarbon resin. Any suitable known process for polymerizing C9 resin can be used and the process may be performed in the presence of any known and suitable catalyst. After the polymerization step, the resulting polymerizate is processed to remove/deactivate the catalyst and to strip out the solvent and any unreacted monomer. The removed solvent can be further separated to remove usable coproducts and at least a portion may be recycled back into the polymerization step for further reuse.

[00112] The resulting crude C9 hydrocarbon resin can optionally be removed from the polymer formation zone as shown in FIG. 7. The recycle content crude C9 hydrocarbon resin from the resin production facility can exhibit at least one, at least two, at least three, at least four, at least five, at least six, at least seven, or all eight of the following characteristics: (i) a weight average molecular weight (Mw) of 1000-1600 g/mol, 1100-1400 g/mol, or 1200-1300 g/mol; (ii) a Gardner Color of less than 12, less than 8, less than 6, less than 4 in a 50% solution with toluene; (iii) a ring and ball softening point of 2-200°C, 5-150°C, 10-125 °C; (iv) a glass transition temperature of less than 100°C, 80°C, 70°C, 60°C, 50°C; (v) a MMAP cloud point of 25-150°C, 40-100°C, 55-90°C; (vi) a DACP cloud point of 1 -100°C, 2-80°C, 5-60°C; (vii) an aromaticity in the range of from 0-60 (5-55, 10-50, 15-45) weight percent aromatic protons, measured by NMR, and (viii) is amorphous.

[00113] Finally, as shown in FIG. 7, the crude C9 hydrocarbon resin from the polymerization zone can be sent to a hydrogenation zone, wherein the resin is hydrogenated via contact with a stream of hydrogen. Any suitable process for resin hydrogenation can be used and, in some embodiments, it may be performed in the presence of a catalyst. In some embodiments, the hydrogen used in the hydrogenation zone can be recycle content hydrogen and can have, for example, a recycle content of at least 10, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 80, at least 90, at least 95, or at least 99 weight percent, based on the total weight of the stream. The recycle content hydrogen can be supplied from any suitable source including, for example, from a gasification facility configured to process hydrocarbon waste. The recycle content applied to the hydrogen can be physical (e.g., molecular) and/or credit- based recycle content, or can originate from the mass balance method. The crude hydrogenated resin can then be subjected to final processing steps (e.g., distillation) to remove any residual solvent and/or catalyst and provide the final recycle content hydrogenated C9 hydrocarbon resin. [00114] In one or more embodiments, the hydrocarbon resin (crude and/or hydrogenated) can be a recycle content hydrocarbon resin having, for example, a recycle content of at least 1 , at least 2, at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.5 weight percent and/or not more than 99, not more than 97, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 5, or not more than 2 weight percent. In some embodiments, the crude and/or hydrogenated hydrocarbon resin can have 100 percent recycle content. [00115] The recycle content hydrogenated C9 hydrocarbon resin from the resin production facility can exhibit at least one, at least two, at least three, at least four, at least five, at least six, at least seven, or all eight of the following characteristics: (i) a weight average molecular weight (Mw) of 1000-1600 g/mol, 1100-1400 g/mol, or 1200-1300 g/mol; (ii) a Gardner Color of less than 4, less than 3, less than 2, less than 1 in a 50% solution with toluene; (iii) a ring and ball softening point of 2-200°C, 5-150°C, 10-125 °C; (iv) a glass transition temperature of less than 100°C, 80°C, 70°C, 60°C, 50°C; (v) a MMAP cloud point of 25-150°C, 40-100°C, 55-90°C; (vi) a DACP cloud point of 1 -100°C, 2- 80°C, 5-60°C; (vii) an aromaticity of not more than 80 percent, 70 percent, 60 percent, or 50 percent, and (viii) is amorphous.

[00116] Referring again to FIG. 1 , the crude and/or hydrogenated recycle content C9 hydrocarbon resin can be used to form one or more products such as, for example, an adhesive. When the hydrocarbon resin is used to form an adhesive composition, it can be introduced into an adhesive production facility as shown in FIG. 1. As discussed previously, the adhesive production facility may or may not be co-located with any of the upstream facilities and may or may not be operated by the same entity. [00117] The adhesive production facility may be any facility configured to produce an adhesive composition. Generally, an adhesive composition comprises a base polymer and a tackifier composition. Other additives to adhesive compositions include, but are not limited to, waxes, oils, plasticizers, and other compounds. The adhesive compositions can include a base polymer in an amount of from 10 to 90, 20 to 80, or 30 to 70 percent of a base polymer, and 1 to 90, 2 to 75, and 5 to 35 weight percent of tackifier, which can be or include a recycle content C9 hydrocarbon resin.

[00118] Examples of suitable base polymers include, but are not limited to, ethylene vinyl acetate copolymer, ethylene n-butyl acrylate copolymer, ethylene methyl acrylate copolymer, polyester, neoprene, acrylics, urethane, poly(acrylate), ethylene acrylic acid copolymer, polyether ether ketone, polyamide, styrenic block copolymers, random styrenic copolymers, hydrogenated styrenic block copolymers, styrene butadiene copolymers, natural rubber, polyisoprene, polyisobutylene, atactic polypropylene, polyethylene including atactic polypropylene, ethylene-propylene polymers, propylene-hexene polymers, ethylene-butene polymers, ethylene octene polymers, propylene-butene polymers, propylene-octene polymers, metallocene-catalyzed polypropylene polymers, metallocene-catalyzed polyethylene polymers, ethylene-propylene-butylene terpolymers, copolymers produced from propylene, ethylene, and various C4-C10 alpha-olefin monomers, polypropylene polymers, functional polymers such as maleated polyolefins, butyl rubber, polyester copolymers, copolyester polymers, isoprene, the terpolymer formed from the monomers ethylene, propylene, and a bicyclic olefin (known as “EPDM”), isoprene-based block copolymers, butadiene-based block copolymers, acrylate copolymers such as ethylene acrylic acid copolymer, butadiene acrylonitrile rubber, and/or polyvinyl acetate.

[00119] The adhesive composition can contain elastomer, tackifier resin, and other additives such as, but not limited to, oils, waxes, plasticizers, antioxidants, and fillers, depending on the end use application. Such additives can be present in an amount of 1 to 75, 5 to 50, or 10 to 40 weight percent, based on the total weight of the composition. [00120] The tackifier in the adhesive composition can be or comprise the recycle content hydrocarbon resin formed in the hydrocarbon resin production facility. Additionally, other tackifier resins (having recycle content or not) can also be present in various embodiments of the described compositions, which are optionally present in the form of physical blends.

[00121] Any suitable method of forming an adhesive composition can be used in the adhesive production facility shown in FIG. 1. For example, in some embodiments, the adhesive composition can be formed by blending a recycle content hydrocarbon resin with an elastomer (e.g., the base polymer) to form the adhesive. As a non-limiting exemplary embodiment, the components of the composition can be blended in a mixer such as a Sigma blade mixer, a plasticorder, a Brabender mixer, a twin-screw extruder, and/or an in-can blend can (pint-cans). In other embodiments, the adhesive composition can be shaped into a desired form, such as a tape or sheet, by an appropriate technique (e.g., extrusion, compression molding, calendaring, or roll coating techniques such as gravure, and reverse roll). In some embodiments, the adhesive compositions can be formed using curtain coating, slot-die coating, or sprayed through different nozzle configurations at different speeds using typical application equipment.

[00122] In one or more embodiments, the recycle content hydrocarbon resins described herein can be utilized in one or more different types of adhesives, such as, for example, hotmelt adhesives, water-based adhesives, solvent based adhesives, hot melt pressure-sensitive adhesives, solvent-based pressure-sensitive adhesives, hot melt nonwoven/hygiene adhesives, and hot melt packaging adhesives. Such adhesives may then be used in an array of end products, including hygienic packaging and other packaging applications. [00123] Turning again to FIG. 1 , in some embodiments, at least a portion of the recycle content adhesive composition from the adhesive production facility can be used to form an end product in an end product facility. The end product facility may or may not be co-located with the adhesive production facility and may or may not be operated by the same entity. In some cases, the end product may not be or comprise an adhesive, but may be or include another modified product such as a tire composition or a coating. In such cases, the recycle content hydrocarbon resin may bypass the adhesive production facility and pass directly from the hydrocarbon resin production facility to the end product production facility.

[00124] The recycle content hydrocarbon resins can be utilized in a wide array of applications including, for example, coatings, sealants, roofing membranes, waterproof membranes and underlayments, carpet, laminated articles, tapes (e.g. tamper evident tapes, water activated tapes, gummed tape, sealing tape, scrim reinforced tape, veneer tape, reinforced and non-reinforced gummed paper tape, box makers tape, paper tape, packaging tape, duct tape, masking tape, invisible tape, electrical tape, gaffer tape, hockey tape, medical tape, etc.), labels (e.g. general purpose label, beverage label, freezer label, smart label, consumer electronics etc.), mastics, polymer blends, wire coatings, molded articles, and rubber additives.

[00125] Furthermore, in various embodiments, the inventive copolymers described herein can also be used to modify existing polymer blends that are typically utilized in plastics, elastomeric applications, roofing applications, cable filling, and tire modifications. The inventive copolymers can improve the adhesion, processability, stability, viscoelasticity, thermal properties, and mechanical properties of these polymer blends.

[00126] When the end product includes a recycle content adhesive, it can be used in, for example, hot melt or solvent based pressure sensitive adhesives, e.g., tapes, labels, mastics, HVACs, and the like, hot melt nonwoven adhesives, e.g., those for use in the construction industry, for elastic attachment, or for stretching, and hot melt packaging adhesives. Furthermore, recycle content hydrocarbon resin compositions as described herein may be incorporated into different polymer systems to provide excellent physical and chemical properties in terms of processability, stability, thermal properties, viscoelasticity, rheology, volatility, fogging profiles, and/or adhesion and mechanical properties of such polymer systems. Moreover, recycle content hydrocarbon resin compositions can be used to enhance various physical and chemical properties in thermoplastic elastomer applications such as roofing applications (construction), adhesives, sealant applications, cable flooding/filling applications, and tire elastomer applications, e.g., tread compositions, side walls, inner liners, inner-tubes, and various other pneumatic tire components. In one or more embodiments, the adhesive composition or end product can have a recycle content of at least 1 , at least 2, at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, at least 97, at least 99, or at least 99.5 weight percent and/or not more than 99, not more than 97, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 5, or not more than 2 weight percent.

[00127] In some embodiments, at least one of the hydrocarbon stream, the pyrolysis fluid, the crude C9 hydrocarbon resin, the hydrogenated C9 hydrocarbon resin, the adhesive, and the end product have a recycle content of at least 10 (20, 30, 40, 50, 60, 70, 80, 90, or 95) weight percent, based on the total weight of the stream, composition, or article, or the recycle content of one or more of these items or streams can be 100 percent.

Recycle Content Products

[00128] As noted above, the present technology relates to hydrocarbon resin compositions, their manufacture and use, and chemical recycling. More particularly, the present technology concerns hydrocarbon resins, adhesive compositions, and end products having recycle content, which is directly or indirectly derived from chemical recycling of hydrocarbon waste and/or bio naphtha. In one or more embodiments herein, the hydrocarbon waste can include waste plastic and/or biowaste and it can be recycled with or without bio naphtha as discussed in detail previously.

[00129] In one or more embodiments, a method is provided for processing a composition derived directly or indirectly from a recycled hydrocarbon waste and/or bio-naphtha (“r-composition”), wherein the method comprises feeding an r-composition to a reactor in which hydrocarbon resins, such as a C9 hydrocarbon resins, are made.

[00130] Generally, the determination of whether an r-composition is derived directly or indirectly from hydrocarbon waste and/or bio-naphtha is not on the basis of whether intermediate steps or entities do or do not exist in the supply chain, but rather whether at least a portion of the r-composition that is fed to the reactor for making a product, such as C9 hydrocarbon resin, can be traced to an r-composition made from and/or formed from hydrocarbon waste and/or bio naphtha.

[00131] As noted herein, the C9 hydrocarbon resin are considered to be directly derived from hydrocarbon waste and/or bio-naphtha if at least a portion of the reactant feedstock used to make the product can be traced back, optionally through one or more intermediate steps or entities, to at least a portion of a r-composition produced from and/or formed from hydrocarbon waste and/or bio-naphtha (e.g., during the cracking of r-pyrolysis oil fed to a cracking furnace or as an effluent from the cracking furnace).

[00132] Generally, an r-composition is considered to be indirectly derived from hydrocarbon waste and/or bio-naphtha if it: (i) has associated with it a recycle content allotment and (ii) may or may not contain a physical component that is traceable to an r-composition at least a portion of which is obtained from hydrocarbon waste and/or bio-naphtha. In one or more embodiments, (i) the manufacturer of the C9 hydrocarbon resin can operate within a legal framework, an association framework, or an industry recognized framework for making a claim to a recycle content through, for instance, a system of credits transferred to the product manufacturer regardless of where or from whom the r- composition or derivatives thereof, or reactant feedstocks to make the product, are purchased or transferred, or (ii) a supplier of the r-composition or a derivate thereof (“supplier”) operates within an allocation framework that allows for applying a recycle content value to a portion or all of the r-composition or derivates thereof (allotment) made with hydrocarbon waste and/or bio-naphtha and transferring the allotment to the manufacturer of the product or any intermediary who obtains a supply of r-composition, or its derivatives, from the supplier. In this system, one need not trace the source of the r-composition volume back to the manufacture of the r-composition from hydrocarbon waste and/or bio-naphtha, but rather can use any hydrocarbon composition made by any process and have associated with such an hydrocarbon composition a recycle content allotment.

[00133] In some embodiments, a pro-rata approach to the mass of r-C9 hydrocarbon directly or indirectly obtained from hydrocarbon waste and/or bio naphtha to the mass of C9 hydrocarbon from other sources may be adopted to determine the percentage in the declaration attributable to r-C9 hydrocarbon obtained directly or indirectly from hydrocarbon waste and/or bio-naphtha. [00134] In one or more embodiments, the C9 hydrocarbon supplier transfers a recycle content allotment to the C9 hydrocarbon resin manufacturer and a supply of C9 hydrocarbon to the C9 hydrocarbon resin manufacturer, where the recycle content allotment is not associated with the C9 hydrocarbon supplied, or even not associated with any C9 hydrocarbon made by the C9 hydrocarbon supplier. This allows flexibility among the C9 hydrocarbon supplier and C9 hydrocarbon resin manufacturer to apportion a recycle content among the variety of products they each make.

[00135] In one or more embodiments, the C9 hydrocarbon supplier transfers a recycle content allotment to the C9 hydrocarbon resin manufacturer and a supply of C9 hydrocarbon to the C9 hydrocarbon resin manufacturer, where the recycle content allotment is associated with C9 hydrocarbon.

[00136] The allotment may be obtained by the C9 hydrocarbon resin manufacturer (or its Family of Entities) from any person or entity without obtaining a supply of C9 hydrocarbon from the person or entity. The person or entity can be a C9 hydrocarbon manufacturer that does not supply C9 hydrocarbon to the C9 hydrocarbon resin manufacturer or its Family of Entities, or the person or entity can be a manufacturer that does not make C9 hydrocarbon.

[00137] In one or more embodiments, the C9 hydrocarbon resin manufacturer can deposit the allotment into a recycle inventory. The C9 hydrocarbon resin manufacturer makes C9 hydrocarbon resin, whether or not a recycle content is applied to the C9 hydrocarbon resin so made and whether or not a recycle content value, if applied to the C9 hydrocarbon resin, is drawn from the recycle inventory.

[00138] If desired, in one or more embodiments, any allotment can be deducted from the recycle inventory and applied to the C9 hydrocarbon resin in any amount and at any time up to the point of sale or transfer of the C9 hydrocarbon resin to a third party. Thus, the recycle content allotment applied to the C9 hydrocarbon resin can be derived directly or indirectly from hydrocarbon waste and/or bio-naphtha, or the recycle content allotment applied to the C9 hydrocarbon resin are not derived directly or indirectly from hydrocarbon waste and/or bio-naphtha.

[00139] In one or more embodiments, a recycle content allotment can include a recycle content allocation or a recycle content credit obtained with the transfer or use of a raw material. For example, in one or more embodiments, an allocation may be deposited into a recycle inventory, and a credit may be withdrawn from an inventory and applied to a composition.

[00140] The C9 hydrocarbon resin composition can be made from any source of a C9 hydrocarbon composition, whether or not the C9 hydrocarbon composition is a r-C9 hydrocarbon, and whether or not the C9 hydrocarbon is obtained from a supplier or made by the C9 hydrocarbon resin manufacturer or within its Family of Entities. Once a C9 hydrocarbon resin composition is made, it can be designated as having recycle content based on and derived from at least a portion of the allotment, again whether or not the r-C9 hydrocarbon is used to make the r-C9 hydrocarbon resin composition and regardless of the source of C9 hydrocarbon used to make the C9 hydrocarbon resin. The allocation can be withdrawn or deducted from recycle inventory. The amount of the deduction and/or applied to the C9 hydrocarbon resin can correspond to any of the methods described above, e.g., a mass balance approach.

[00141] In one or more embodiments, recycle content C9 hydrocarbon resin composition can be made by reacting a C9 hydrocarbon composition obtained from any source in a synthetic process to make C9 hydrocarbon resin, and a recycle content value can be applied to at least a portion of the C9 hydrocarbon resin to thereby obtain r-C9 hydrocarbon resin. Optionally, a recycle content value can be obtained by deducting from a recycle inventory. The entire amount of recycle content value in the C9 hydrocarbon resin can correspond to the recycle content value deducted from the recycle inventory. Recycle content value deducted from the recycle inventory can be applied to both C9 hydrocarbon resin and products or compositions other than C9 hydrocarbon resin made by the C9 hydrocarbon resin manufacturer or a person or entity among its Family of Entities. The C9 hydrocarbon composition can be obtained from a third party, or made by the C9 hydrocarbon resin manufacturer, or made by a person or entity amount the Family of Entities of the C9 hydrocarbon resin manufacturer and transferred to the C9 hydrocarbon resin manufacturer. [00142] The recycle content in the first r-C9 hydrocarbon resin need not be obtained from a recycle inventory, but rather can be attributed to C9 hydrocarbon resin by any of the methods described herein (e.g., by virtue of using a r-C9 hydrocarbon as a reactant feed), and the C9 hydrocarbon resin manufacturer may seek to further increase the recycle content in the first r-C9 hydrocarbon resin so made. In another example, a C9 hydrocarbon resin distributor may have r-C9 hydrocarbon resin in its inventory and seek to increase the recycle content value of the first r-C9 hydrocarbon resin in its possession. The recycle content in the first r-C9 hydrocarbon resin can be increased by applying a recycle content value withdrawn from a recycle inventory.

[00143] Some C9 hydrocarbon resin manufacturers may be integrated into making downstream products using C9 hydrocarbon resin as adhesives or end products such as textiles, labels, tapes, and woodworking articles that use such adhesives. They, and other non-integrated C9 hydrocarbon resin manufacturers, can also offer to sell or sell C9 hydrocarbon resin on the market as containing or obtained with an amount of recycle content. The recycle content designation can also be found on or in association with the downstream product made with the C9 hydrocarbon resin, such as an adhesive or an end product including an adhesive. [00144] In one or more embodiments, the amount of recycle content in the r- C9 hydrocarbon and/or in the r-C9 hydrocarbon resin will be based on the allocation or credit obtained by the manufacturer of the C9 hydrocarbon resin composition or the amount available in the C9 hydrocarbon resin manufacturer’s recycle inventory. A portion or all of the recycle content value in an allocation or credit obtained by or in the possession of a manufacturer of C9 hydrocarbon resin can be designated and assigned to an r-C9 hydrocarbon or r-C9 hydrocarbon resin on a mass balance basis.

[00145] The allotment can be obtained from a variety of sources in the manufacturing chain starting from pyrolyzing hydrocarbon waste and/or cracking bio-naphtha up to making and selling a r-C9 hydrocarbon. The recycle content value applied to C9 hydrocarbon resin or the allocation deposited into the recycle inventory need not be associated with r-C9 hydrocarbon. In one or more embodiments, the process for making r-C9 hydrocarbon resin can be flexible and allow for obtaining an allocation anywhere along the manufacturing chain to make C9 hydrocarbon resin starting from pyrolyzing hydrocarbon waste and/or cracking pyrolysis oil, pyrolysis gas, or bio-naphtha.

[00146] In one or more embodiments, a system or package is provided that comprises: C9 hydrocarbon resin, and an identifier associated with the C9 hydrocarbon resin, the identifier being a representation that the C9 hydrocarbon resin have recycle content or is made from a source having recycle content. [00147] The package can be any suitable package for containing C9 hydrocarbon resin, such as a plastic or metal drum, railroad car, isotainer, totes, polytotes, IBC totes, bottles, jerricans, and polybags. The identifier can be a certificate document, a product specification stating the recycle content, a label, a logo or certification mark from a certification agency representing that the article or package contains contents or the C9 hydrocarbon resin contains, or is made from sources or associated with recycle content, or it can be electronic statements by the C9 hydrocarbon resin manufacturer that accompany a purchase order or the product, or posted on a website as a statement, representation, or a logo representing that the C9 hydrocarbon resin contains or is made from sources that are associated with or contain recycle content, or it can be an advertisement transmitted electronically, by or in a website, by email, or by television, or through a tradeshow, in each case that is associated with C9 hydrocarbon resin.

[00148] In one or more embodiments, the r-C9 hydrocarbon resin, or articles made thereby, can be offered for sale or sold as C9 hydrocarbon resin containing or obtained with, or an article containing or obtained with, recycle content. The sale or offer for sale can be accompanied with a certification or representation of the recycle content claim made in association with the C9 hydrocarbon resin or article made with the C9 hydrocarbon resin.

[00149] In one or more embodiments, the composition receiving the recycle content allotment can be a non-recycle composition.

[00150] The C9 hydrocarbon can be stored in a storage vessel and transferred to a C9 hydrocarbon resin manufacturing facility by way of truck, pipe, or ship, or as further described below, the C9 hydrocarbon production facility can be integrated with the C9 hydrocarbon resin facility. The C9 hydrocarbon may be shipped or transferred to the operator or facility that makes the C9 hydrocarbon resin.

[00151] In one or more embodiments, one may integrate two or more facilities and make r-C9 hydrocarbon resin. The facilities to make r-C9 hydrocarbon resin, the C9 hydrocarbon, and the r-pyoil and/or r-pyrolysis gas, can be stand alone facilities or facilities integrated to each other. For example, one may establish a system of producing and consuming a recycle C9 hydrocarbon composition at least a portion of which is obtained from directly or indirectly from cracking r-pyoil or obtaining r-pyrolysis gas.

[00152] The C9 hydrocarbon resin manufacturing facility can make r-C9 hydrocarbon resin, and can make the r-C9 hydrocarbon resin directly or indirectly from the pyrolysis of hydrocarbon waste, cracking of bio-naphtha, and/or the cracking of r-pyoil and/or r-pyrolysis gas. For example, in a direct method, the C9 hydrocarbon resin manufacturing facility can make r-C9 hydrocarbon resin by accepting r-C9 hydrocarbon from the C9 hydrocarbon manufacturing facility and feeding the r-C9 hydrocarbon as a feed stream to a reactor to make C9 hydrocarbon resin. Alternatively, the C9 hydrocarbon resin manufacturing facility can make r-C9 hydrocarbon resin by accepting any C9 hydrocarbon composition from the C9 hydrocarbon manufacturing facility and applying a recycle content to C9 hydrocarbon resin made with the C9 hydrocarbon composition by deducting recycle content value from its recycle inventory and applying them to the C9 hydrocarbon resin, optionally in amounts using the methods described above. The allotments obtained and stored in recycle inventory can be obtained by any of the methods described above, and need not necessarily be allotments associated with r-C9 hydrocarbon.

[00153] In one or more embodiments, the integrated process includes at least two facilities co-located within 5, within 3, within 2, or within 1 mile of each other (measured as a straight line). In one or more embodiments, at least two facilities are owned by the same Family of Entities.

[00154] A C9 hydrocarbon resin manufacturer or its Family of Entities can obtain a recycle content allocation, and the allocation can be obtained by any of the means described herein and can be deposited into recycle inventory, the recycle content allocation derived directly or indirectly from pyrolyzing a hydrocarbon waste, cracking a bio-naphtha, cracking r-pyrolysis oil, and/or separating a r-pyrolysis gas. The C9 hydrocarbon converted in a synthetic process to make a C9 hydrocarbon resin composition can be any C9 hydrocarbon composition obtained from any source, including a non-r-C9 hydrocarbon composition, or it can be a r-C9 hydrocarbon composition. The r- C9 hydrocarbon resin sold or offered for sale can be designated (e.g., labelled or certified or otherwise associated) as having a recycle content value.

[00155] In one or more embodiments, at least a portion of the recycle content value associated with the r-C9 hydrocarbon resin can be drawn from a recycle inventory. Alternatively, in one or more embodiments, at least a portion of the recycle content value in the C9 hydrocarbon resin are obtained by converting r-C9 hydrocarbon. For example, the recycle content value deducted from the recycle inventory can be a non-pyrolysis recycle content value or can be a pyrolysis recycle content allocation (i.e., a recycle content value that has its origin in pyrolysis of hydrocarbon waste and/or cracking of bio-naphtha). The recycle inventory can optionally contain at least one entry that is an allocation derived directly or indirectly from pyrolyzing a hydrocarbon waste, cracking a bio-naphtha, cracking r-pyrolysis oil, and/or separating a r-pyrolysis gas. The designation can be the amount of allocation deducted from recycle inventory, or the amount of recycle content declared or determined by the C9 hydrocarbon resin manufacturer in its accounts. The amount of recycle content does not necessarily have to be applied to the C9 hydrocarbon resin in a physical fashion. The designation can be an internal designation to or by the C9 hydrocarbon resin manufacturer or its Family of Entities or a service provider in contractual relationship to the C9 hydrocarbon resin manufacturer or its Family of Entities. The amount of recycle content represented as contained in the C9 hydrocarbon resin sold or offered for sale has a relationship or linkage to the designation. The amount of recycle content can be a 1 :1 relationship in the amount of recycle content declared on C9 hydrocarbon resin offered for sale or sold and the amount of recycle content assigned or designated to the C9 hydrocarbon resin by the C9 hydrocarbon resin manufacturer.

[00156] In one or more embodiments, the C9 hydrocarbon resin composition can have associated with it, contains, labelled, advertised, and/or certified as containing recycle content in an amount of at least 0.005, at least 0.01 , at least 0.05, at least 0.1 , at least 0.2, at least 0.25, at least 0.3, at least 0.35, at least 0.4, at least 0.45, at least 0.5, at least 0.6, at least 0.7, at least 0.8, at least 0.9, at least 1 , at least 2, at least 3, at least 4, at least 5, at least 6, at least 7, at least 8, at least 9, at least 10, at least 11 , at least 13, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, at least 98, or at least 99 weight percent.

[00157] Additionally, or in the alternative, in one or more embodiments, the C9 hydrocarbon resin composition can have associated with it, contains, labelled, advertised, and/or certified as containing recycle content in an amount of not more than 100, not more than 98, not more than 95, not more than 90, not more than 85, not more than 80, not more than 75, not more than 70, not more than 65, not more than 60, not more than 55, not more than 50, not more than 45, not more than 40, not more than 35, not more than 30, not more than 25, not more than 20, not more than 15, not more than 10, not more than 9, not more than 8, not more than 7, not more than 6, not more than 5, not more than 4, not more than 3, not more than 2, not more than 1 , not more than 0.9, not more than 0.8, not more than 0.7, not more than 0.6, or not more than 0.5 weight percent.

[00158] The recycle content associated with the C9 hydrocarbon resin can be established by applying a recycle content value to the C9 hydrocarbon resin, such as through deducting the recycle content value from a recycle inventory populated with allotments (credit or allocation) or by reacting a r-C9 hydrocarbon feedstock to make r-C9 hydrocarbon resin. The allotment can be contained in a recycle inventory created, maintained, or operated by or for the C9 hydrocarbon resin manufacturer. The allotments may be obtained from any source along any manufacturing chain of products. In certain embodiments, the origin of the allotment is derived indirectly from pyrolyzing a hydrocarbon waste, cracking bio-naphtha, cracking r-pyrolysis oil, and/or separating a r- pyrolysis gas.

[00159] There is provided a process for making a recycle content adhesive that includes the steps of: obtaining a recycle content C9 hydrocarbon resin; making an adhesive comprising a C9 hydrocarbon resin; and applying a recycle content allotment to the adhesive to obtain a recycle content adhesive.

[00160] There is also provided a process for making a recycle content adhesive that includes the steps of: obtaining a recycle content adhesive having recycle content derived directly or indirectly from a recycle content C9 hydrocarbon resin; making an end product comprising an adhesive; and applying a recycle content allotment to the end product to obtain the recycle content end product.

[00161] In some embodiments, there is provided a step of collecting one or more used (post-consumer or post-industrial) end products including an adhesive comprising a C9 hydrocarbon resin and supplying at least a portion of the collected end products to a pyrolysis unit and/or pyrolyzing at least a portion of the end products to form a recycle content pyrolysis fluid as discussed previously. Additionally, or in the alternative, upon collection of the end products, a recycle content allocation may be obtained, which may be applied to one or more streams as discussed herein. For example, the collector (which may also be the manufacturer of the end product) may also make more of the same end product and apply a recycle content allotment to the manufactured end products to thereby provide a recycle content end product. Alternatively, the operator of the pyrolysis facility (or other entity receiving the collected end products) may make or obtain a recycle content allotment, which can be applied to a stream produced by that operator (e.g., pyrolysis gas or pyrolysis oil).

Definitions

[00162] It should be understood that the following is not intended to be an exclusive list of defined terms. Other definitions may be provided in the foregoing description, such as, for example, when accompanying the use of a defined term in context.

[00163] As used herein, the terms “a,” “an,” and “the” mean one or more. [00164] As used herein, the term “and/or,” when used in a list of two or more items, means that any one of the listed items can be employed by itself or any combination of two or more of the listed items can be employed. For example, if a composition is described as containing components A, B, and/or C, the composition can contain A alone; B alone; C alone; A and B in combination; A and C in combination, B and C in combination; or A, B, and C in combination. [00165] As used herein, the phrase “at least a portion” includes at least a portion and up to and including the entire amount or time period.

[00166] As used herein, the terms “comprising,” “comprises,” and “comprise” are open-ended transition terms used to transition from a subject recited before the term to one or more elements recited after the term, where the element or elements listed after the transition term are not necessarily the only elements that make up the subject.

[00167] As used herein, the term “directly derived” refers to having at least one physical component originating from waste plastic. [00168] As used herein, the term “enriched” refers to having a concentration (on a dry weight basis) of a specific component that is greater than the concentration of that component in a reference material or stream.

[00169] As used herein, the term “Family of Entities” means at least one person or entity that directly or indirectly controls, is controlled by, or is under common control with another person or entity, where control means ownership of at least 50% of the voting shares, or shared management, common use of facilities, equipment, and employees, or family interest. As used throughout, the mention of a person or entity provides claim support for and includes any person or entity among the Family of Entities.

[00170] As used herein, the terms “having,” “has,” and “have” have the same open-ended meaning as “comprising,” “comprises,” and “comprise” provided above.

[00171] As used herein, the terms “including,” “include,” and “included” have the same open-ended meaning as “comprising,” “comprises,” and “comprise” provided above.

[00172] As used herein, the term “indirectly derived” refers to having an assigned recycle content i) that is attributable to hydrocarbon waste or bio naphtha, but ii) that is not based on having a physical component originating from waste plastic.

[00173] As used herein, the terms “mixed plastic waste” and “MPW” refer to a mixture of at least two types of waste plastics including, but not limited to the following plastic types: polyethylene terephthalate (PET), one or more polyolefins (PO), and polyvinylchloride (PVC).

[00174] As used herein, "non-recycle" means a composition (e.g., compound, polymer, feedstock, product, or stream) none of which was directly or indirectly derived from recycled hydrocarbon waste or bio-naphtha.

[00175] As used herein, the term “predominantly” means more than 50 percent by weight. For example, a predominantly propane stream, composition, feedstock, or product is a stream, composition, feedstock, or product that contains more than 50 weight percent propane. [00176] As used herein, the term “pyrolysis” refers to thermal decomposition of one or more organic materials at elevated temperatures in an inert (i.e., substantially oxygen free) atmosphere.

[00177] As used herein, the term “pyrolysis gas” refers to a composition obtained from pyrolysis that is gaseous at 25°C.

[00178] As used herein, the terms “pyrolysis oil” or “pyoil” refers to a composition obtained from pyrolysis that is liquid at 25°C and 1 atm.

[00179] As used herein, the term “pyrolysis residue” refers to a composition obtained from pyrolysis that is not pyrolysis gas or pyrolysis oil and that comprises predominantly pyrolysis char and pyrolysis heavy waxes.

[00180] As used herein, the term “recycle content” and “r-content” refer to being or comprising a composition that is directly and/or indirectly derived from hydrocarbon waste and/or bio-naphtha.

[00181] As used herein, “recycle content allocation” and “allocation” mean a type of recycle content allotment, where the entity or person supplying a composition sells or transfers the composition to the receiving person or entity, and the person or entity that made the composition has an allotment at least a portion of which can be associated with the composition sold or transferred by the supplying person or entity to the receiving person or entity. The supplying entity or person can be controlled by the same entity or person(s) or a variety of affiliates that are ultimately controlled or owned at least in part by a parent entity (“Family of Entities”), or they can be from a different Family of Entities. Generally, a recycle content allocation travels with a composition and with the downstream derivates of the composition. An allocation may be deposited into a recycle inventory and withdrawn from the recycle inventory as an allocation and applied to a composition if the composition is made by the particular feedstock from which the deposited allocation was deposited into the recycle inventory.

[00182] As used herein, “recycle content allotment” and “allotment” refer a recycle content value that is: (a) transferred from an originating composition (e.g., compound, polymer, feedstock, product, or stream), at least a portion of which is obtained from recycled hydrocarbon waste or bio-naphtha or which has a recycle content value at least a portion of which originates from a recycled hydrocarbon waste or bio-naphtha, to a receiving composition (e.g., compound, polymer, feedstock, product, or stream) that may or may not have a physical component that is traceable to a composition at least a portion of which is obtained from a recycled hydrocarbon waste or bio-naphtha; or (b) deposited into a recycle inventory from an originating composition (e.g., compound, polymer, feedstock, product, or stream) at least a portion of which is obtained from or having a recycle content value, at least a portion of which originates from a recycled hydrocarbon waste or bio-naphtha. It should be noted that a recycle content allotment can include a recycle content allocation or a recycle content credit obtained with the transfer or use of a raw material.

[00183] As used herein, the terms “recycle content composition,” “recycle composition,” and “r-composition” mean a composition having recycle content. [00184] As used herein, “recycle content credit” and “credit” mean a type of recycle content allotment, where the allotment is available for sale or transfer or use, or is sold or transferred or used, either: (a) without the sale of a composition, (b) with the sale or transfer of a composition but the allotment is not associated the sale or transfer of the composition, or (c) is deposited into or withdrawn from a recycle inventory that does not track the molecules of a recycle content feedstock to the molecules of the resulting compositions which were made with the recycle content feedstocks, or which does have such tracking capability but which did not track the particular allotment as applied to a composition.

[00185] As used herein, “recycle inventory” and “inventory” refer to a group or collection of allotments (allocations or credits) from which deposits and deductions of allotments in any units can be tracked. The inventory can be in any form (electronic or paper), using any or multiple software programs, or using a variety of modules or applications that together as a whole tracks the deposits and deductions. Desirably, the total amount of recycle content withdrawn (or applied to compositions) does not exceed the total amount of recycle content allotments on deposit in the recycle content inventory (from any source, not only from cracking of r-pyoil). However, if a deficit of recycle content value is realized, the recycle content inventory is rebalanced to achieve a zero or positive recycle content value available. The timing for rebalancing can be either determined and managed in accordance with the rules of a particular system of accreditation adopted by the end product manufacturer or by one among its Family of Entities, or alternatively, is rebalanced within one (1 ) year, or within six (6) months, or within three (3) months, or within one (1 ) month of realizing the deficit. The timing for depositing an allotment into the recycle content inventory, applying an allotment (or credit) to a composition to make a r-composition, and cracking r-pyoil, need not be simultaneous or in any particular order. In one embodiment or in combination with any mentioned embodiments, the step of cracking a particular volume of r-pyoil occurs after the recycle content value or allotment from that volume of r-pyoil is deposited into a recycle content inventory. Further, the allotments or recycle content values withdrawn from the recycle content inventory need not be traceable to r-pyoil or cracking r-pyoil, but rather can be obtained from any waste recycle stream, and from any method of processing the recycle waste stream. Desirably, at least a portion of the recycle content value in the recycle content inventory is obtained from r-pyoil, and optionally at least a portion of r-pyoil, are processed in the one or more cracking processes as described herein, optionally within a year of each other and optionally at least a portion of the volume of r-pyoil from which a recycle content value is deposited into the recycle content inventory is also processed by any or more of the cracking processes described herein.

[00186] As used herein, a “Site” refers to the largest continuous geographical boundary owned by a hydrogen manufacturer, or by one person or entity, or combination of persons or entities, among its Family of Entities, wherein the geographical boundary contains one or more manufacturing facilities at least one of which is a cracking, a resin production facility, an adhesive production facility, or an end product production facility.

[00187] As used herein, the terms “waste plastic” and “plastic waste” refer to used, scrap, and/or discarded plastic materials. The waste plastic may be unprocessed or partially processed. [00188] As used herein, the phrase “at least a portion” includes at least a portion and up to and including the entire amount or time period.

[00189] As used herein, “downstream” means a target unit operation, vessel, or equipment that: a. is in fluid (liquid or gas) communication, or in piping communication, with an outlet stream from the radiant section of a cracker furnace, optionally through one or more intermediate unit operations, vessels, or equipment, or b. was in fluid (liquid or gas) communication, or in piping communication, with an outlet stream from the radiant section of a cracker furnace, optionally through one or more intermediate unit operations, vessels, or equipment, provided that the target unit operation, vessel, or equipment remains within the battery limits of the cracker facility (which includes the furnace and all associated downstream separation equipment).

CLAIMS NOT LIMITED TO DISCLOSED EMBODIMENTS [00190] The preferred forms of the invention described above are to be used as illustration only and should not be used in a limiting sense to interpret the scope of the present invention. Modifications to the exemplary embodiments, set forth above, could be readily made by those skilled in the art without departing from the spirit of the present invention.

[00191] The inventors hereby state their intent to rely on the Doctrine of Equivalents to determine and assess the reasonably fair scope of the present invention as it pertains to any apparatus not materially departing from but outside the literal scope of the invention as set forth in the following claims.