MÉTODOS DE REGENERAÇÃO DE CATALISADORES DE AROMATIZAÇÃO

Abstract

Methods of regenerating spent catalysts, such as spent aromatization catalysts, which may include a transition metal and a catalyst support. The methods may include contacting a catalyst with a fluorine-containing stream that includes a fluorine-containing compound. The fluorine-containing compound may include a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC), a fluorocarbon (FC), or a combination thereof.

Description

1 / 91 METHODS FOR REGENERATING FLAVORING CATALYSTS CROSS-REFERENCE TO RELATED REQUESTS

[0001] This application claims priority over U.S. Provisional Patent Application No. 63 / 568,189, filed March 21, 2024, U.S. Provisional Patent Application No. 63 / 493,418, filed March 31, 2023, and U.S. Provisional Patent Application No. 63 / 491,703, filed March 22, 2023, which are incorporated herein by reference. TECHNICAL FIELD OF THE INVENTION

[0002] This disclosure relates to methods for regenerating spent aromatization catalysts and their use in the aromatization of aliphatic hydrocarbons into aromatic hydrocarbons. FUNDAMENTALS

[0003] Aromatization catalysts can be regenerated with processes that include chlorination, oxidation, and fluorination. Fluorination is typically carried out with a fluorination source that includes gaseous fluorine in nitrogen, which can be disadvantageous, especially with regard to the distribution of fluorine through a catalyst bed. Fluorine can react with a catalyst upon contact, so that a leading edge of a catalyst bed may have a higher concentration of fluorine than the rest of the bed. In some cases, most, if not all, of the fluorine may be adsorbed by a catalyst, with little or no fluorine advance into the bed.

[0004] There remains a need for improved methods of regenerating aromatization catalysts, including methods that overcome one or more of the previous disadvantages regarding the use of fluorine in a fluorination step. SUMMARY

[0005] This summary is provided to present a selection of concepts that are better described below in the detailed description. This summary is not intended to identify necessary or essential features of Petition 870250083407, dated 09 / 16 / 2025, pages 203 / 309 2 / 91 matter claimed, nor is it intended to limit the scope of the matter claimed.

[0006] Methods for regenerating aromatization catalysts are provided in this document, which may include the use of a fluorine-containing compound instead of fluorine in a fluorination step. The use of the fluorine-containing compounds in this document may improve the distribution of fluorine throughout a catalyst bed.

[0007] In one aspect, methods are provided for regenerating a catalyst, such as a spent aromatization catalyst. The spent catalyst may include a transition metal and a catalyst support in a metal reactor. In some embodiments, the methods include any two or more of the (A)-(H) steps: (A) contacting a hydrocarbon feed with an aromatization catalyst including a transition metal and a catalyst support under reforming conditions in a metal reactor system to produce an aromatic product; (B) carrying out step (A) for a period of time sufficient to form a spent catalyst; (C) contacting the spent catalyst with hydrogen gas to produce a removed spent catalyst;(D) subjecting the removed spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding about 500°F, for a time effective to remove from the spent catalyst at least a portion of the hydrogen carbon feed, at least a portion of the aromatic product, or a combination thereof, to form a treated spent catalyst; (E) contacting the treated spent catalyst with a chlorine-containing stream including a chlorine-containing compound to produce a chlorinated spent catalyst; (F) subjecting the chlorinated spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding 900°F, for a time effective to improve a dispersion of the transition metal in the chlorinated spent catalyst to form a redistributed spent catalyst; (G) contacting the redistributed spent catalyst with a fluorine-containing stream including a fluorine-containing compound to form a regenerated catalyst; and (H) reducing the regenerated catalyst. Petition 870250083407, dated 09 / 16 / 2025, pages 204 / 309 3 / 91

[0008] In some embodiments, the methods include contacting a spent catalyst with a chlorine-containing stream including a chlorine-containing compound to produce a chlorinated spent catalyst; contacting the chlorinated spent catalyst with a decoking gas stream including oxygen to produce a decoked catalyst; and contacting the decoked catalyst with a fluorine-containing stream including a fluorine-containing compound to produce a regenerated catalyst. In some embodiments, the fluorine-containing compound includes a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC), a fluorocarbon (FC), or a combination thereof.

[0009] In another aspect, reactivated catalysts and regenerated catalysts are provided, such as those produced by any of the methods described in this document.

[0010] In yet another aspect, methods are provided for contacting a reactivated catalyst or a regenerated catalyst and a hydrocarbon to produce a product.

[0011] In yet another aspect, methods are provided for contacting a spent catalyst with a stream containing fluorine.In some embodiments, the methods include (a) providing two or more reactors in fluid communication with each other, wherein the two or more reactors are connected in a series, thus allowing a stream containing fluorine to be (i) injected at a selected injection point from one or more injection points, (ii) circulated sequentially through each of the two or more reactors downstream of the injection point, (iii) returned to a first of the two or more reactors and, optionally, (iv) recirculated sequentially through each of the two or more reactors, wherein each of the two or more reactors includes a reservoir in which a spent catalyst is disposed; (b) heating one of the two or more reactors to a temperature that is equal to or greater than a fluorination temperature, and maintaining each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature, wherein the temperature. Petition 870250083407, dated 09 / 16 / 2025, pp. 205 / 309 4 / 91 Fluorination is effective in at least partially decomposing a fluorine-containing compound from the fluorine-containing stream; and (c) injecting the fluorine-containing stream and circulating or recirculating the fluorine-containing stream for an effective time to achieve a desired level of fluorination of the spent catalyst in one of two or more reactors at a temperature that is equal to or greater than the fluorination temperature. The methods may also include (d) heating one different of the two or more reactors to a temperature that is equal to or greater than the fluorination temperature and maintaining each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature; and (e) injecting the fluorine-containing stream and circulating or recirculating the fluorine-containing stream for an effective time to achieve a desired level of fluorination of the spent catalyst in the different of the two or more reactors at a temperature that is equal to or greater than the fluorination temperature.

[0012] In a further aspect, systems are provided for fluorinating a spent catalyst. In some embodiments, the systems include (a) two or more reactors and (b) two or more heating devices. The two or more reactors may be in fluid communication with each other and connected in series. This configuration may allow a fluid stream, such as a stream containing fluorine, to be (i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to a first of the two or more reactors and, optionally, (iv) sequentially recirculated through each of the two or more reactors. The two or more heating devices may be configured to heat each of the two or more reactors to equal or different temperatures.For example, reactors and devices can be coupled in such a way that a reactor is coupled to a heating device.

[0013] Additional aspects will be presented in part in the description that follows, and in part will be obvious from the description, or can be learned by practicing the aspects described in this document. As Petition 870250083407, dated 09 / 16 / 2025, pages 206 / 309 5 / 91 The advantages described in this document can be realized and achieved through the elements and combinations specifically indicated in the appended claims. It should be understood that both the general description above and the detailed description below are exemplary and explanatory only and are not restrictive. BRIEF DESCRIPTION OF THE FIGURES

[0014] FIG. 1 represents an embodiment of a system provided in this document, which can be used to perform one or more embodiments of contact between a spent catalyst and a fluorine-containing stream.

[0015] FIG. 2 represents a graph of the adjusted catalyst temperature as a function of time for an embodiment of a catalyst subjected to an embodiment of the methods described in this document.

[0016] FIG. 3 represents a graph of aromatic selectivity as a function of time for an embodiment of a catalyst subjected to an embodiment of the methods described in this document.

[0017] FIG. 4 represents a graph of the adjusted catalyst temperature as a function of time for (1) an embodiment of a fresh flavoring catalyst, (2) an embodiment of a spent flavoring catalyst and (3) an embodiment of a spent flavoring catalyst subjected to the reactivation procedure described in this document in Example 1C.

[0018] FIG. 5 represents a graph of aromatic selectivity as a function of time for (1) an embodiment of a fresh flavoring catalyst, (2) an embodiment of a spent flavoring catalyst and (3) an embodiment of a spent flavoring catalyst subjected to the embodiment of the reactivation procedure described in this document in Example 1C.

[0019] FIG. 6 represents a graph of the adjusted catalyst temperature as a function of time for (1) an embodiment of a fresh flavoring catalyst, (2) an embodiment of a flavoring catalyst Petition 870250083407, dated 09 / 16 / 2025, pages 207 / 309 6 / 91 spent and (3) a spent flavoring catalyst subjected to the reactivation procedure embodiment described in this document in Example 1D.

[0020] FIG. 7 represents a graph of aromatic selectivity as a function of time for (1) an embodiment of a fresh flavoring catalyst, (2) an embodiment of a spent flavoring catalyst and (3) a spent flavoring catalyst subjected to the embodiment of the reactivation procedure represented in Example 1D. DEFINITIONS

[0021] To define more clearly the terms used in this document, the following definitions are provided. Unless otherwise indicated, the following definitions apply to this disclosure. If a term is used in this disclosure but is not specifically defined in this document, the definition from the IUPAC Compendium of Chemical Terminology, 2nd Ed. (1997) may be applied, provided that such definition does not conflict with any other disclosure or definition applied in this document, or render undefined or ineffective any claim to which such definition applies. To the extent that any definition or usage provided by any document incorporated herein by reference conflicts with the definition or usage provided in this document, the definition or usage provided in this document controls.

[0022] As the various features of the subject matter of this disclosure are described, within a particular aspect, a combination or combinations of the different features may be foreseen. For each aspect of each feature disclosed in this document, all combinations that do not negatively affect the designs, compositions, systems, processes, or methods described in this document are contemplated, with or without the express description of that particular combination. Therefore, unless explicitly indicated otherwise, any aspect of the feature disclosed herein may be combined to describe and disclose consistent inventive designs, compositions, systems, processes, or methods. Petition 870250083407, dated 09 / 16 / 2025, pp. 208 / 309 7 / 91 with all the publicity.

[0023] Although compositions and methods are described in this document under “comprising” various components or steps, compositions and methods may also “consist essentially of” or “consist of” various components or steps, unless stated otherwise.

[0024] The terms including, with and having, as used in this document, are defined as comprising (i.e., open language), unless otherwise specified.

[0025] The terms a, an, and the like are intended to include plural alternatives, for example, at least one. For example, the disclosure of a compound containing fluorine, a catalyst and the like is intended to cover one, or mixtures or combinations of more than one compound containing fluorine, a catalyst and the like, unless otherwise specified.

[0026] Various number ranges are disclosed in this document. When the Applicants disclose or claim a range of any kind, the Applicants' intention is to disclose or claim individually every possible number that such range may reasonably encompass, including range endpoints, as well as any sub-ranges and combinations of sub-ranges encompassed therein, unless otherwise specified. For example, when disclosing a percentage by weight of 1.0% by weight to 2.0% by weight, or 1% by weight to 2% by weight, the Applicant's intention is to individually recite 1.0% by weight, 1.1% by weight, 1.2% by weight, 1.3% by weight, 1.4% by weight, 1.5% by weight, 1.6% by weight, 1.7% by weight, 1.8% by weight, 1.9% by weight and 2.0% by weight, including any subranges and combinations of subranges encompassed therein, and these methods of describing such ranges are interchangeable.Furthermore, all numerical endpoints of the ranges disclosed in this document are approximate, unless excluded by condition. As a representative example, if Applicants state that one or more steps in the processes disclosed in this document can be reduced to one. Petition 870250083407, dated 09 / 16 / 2025, pp. 209 / 309 8 / 91 temperature in a range of 10°C to 75°C, this range should be interpreted as encompassing temperatures in a range of approximately 10°C to approximately 75°C, unless otherwise indicated.

[0027] Values ​​or ranges may be expressed in this document as approximately, approximately a particular value, and / or approximately another particular value. When such values ​​or ranges are expressed, other disclosed modalities include the specific value recited, from a particular value, and / or to another particular value. Similarly, when values ​​are expressed as approximations, by using the antecedent approximately, it will be understood that the particular value forms another modality. It will also be understood that there is a series of values ​​disclosed here and that each value is also disclosed here as approximately that particular value in addition to the value itself. In another aspect, each use of the term approximately may independently mean ±20% of the stated value, ±15% of the stated value, ±10% of the stated value, ±5% of the stated value, or ±3% of the stated value.

[0028] The Applicants reserve the right to exclude or disclaim any individual members of any group of values ​​or ranges, including any sub-ranges or combinations of sub-ranges within the group, that may be claimed in accordance with a range or in any similar manner, if for any reason the Applicants choose to claim less than the full measure of disclosure, for example, to explain a reference that the Applicants may not have known at the time of filing the application. Furthermore, the Applicants reserve the right to exclude or disclaim any individual substitutes, analogues, composites, linkers, structures or groups thereof, or any members of a claimed group, if for any reason the Applicants choose to claim less than the full measure of disclosure, for example, to explain a prior reference or disclosure that the Applicants may not have known at the time of filing the application.

[0029] For any particular compound or group disclosed in this Petition 870250083407, dated 09 / 16 / 2025, pp. 210 / 309 9 / 91 document, any name or structure (general or specific) presented is intended to encompass all isomers, regioisomers, conformational stereoisomers, and mixtures thereof that may arise from a particular set of substituents, unless otherwise specified. The name or structure also encompasses all enantiomers, diastereomers, and other optical isomers (if any), whether in enantiomeric or racemic forms, as well as mixtures of stereoisomers, as would be recognized by one skilled in the art, unless otherwise specified. For example, a general reference to hexane or hexanes includes n-hexane, 2-methylpentane, 3-methylpentane, 2,2-dimethylbutane, and 2,3-dimethylbutane; and a general reference to a butyl group includes an n-butyl group, a sec-butyl group, an iso-butyl group, and a t-butyl group.

[0030] The term substituted when used to describe a group, for example, when referring to a substituted analogue of a particular group, is intended to describe the compound or group in which any non-hydrogen moiety formally replaces the hydrogen in that group or compound and is intended to be non-limiting. A compound or group may also be referred to in this document as non-substituted or by equivalent terms such as non-substituted, which refers to the original group or compound. Substituted is intended to be non-limiting and includes inorganic substituents or organic substituents as specified and as understood by one skilled in the art.

[0031] The terms contact product, contact, and the like are used in this document to describe compositions and methods in which components are contacted together in any order, in any manner, and for any period of time, unless otherwise specified. For example, components may be contacted by mixing or blending. Furthermore, unless otherwise specified, contact of any component may occur in the presence or absence of any other component of the compositions and methods described herein. The combining of additional materials or components may be done by any method. Petition 870250083407, dated 09 / 16 / 2025, pp. 211 / 309 10 / 91 appropriate. Furthermore, the term contact product includes mixtures, blends, solutions, pastes, reaction products and the like, or combinations thereof. Although the contact product may, and often does, include reaction products, it is not necessary that the respective components react with each other. Similarly, contacting two or more components may result in a reaction product or a reaction mixture. Consequently, depending on the circumstances, a contact product may be a mixture, a reaction mixture, or a reaction product.

[0032] Conditions for flavoring aliphatic hydrocarbons means conditions for flavoring at least a portion of the aliphatic hydrocarbons in a feedstock containing aliphatic hydrocarbons when in contact with a catalyst as described herein, such that the catalyst bed discharge comprises at least some aromatic hydrocarbons. Some unreacted aliphatic hydrocarbons will also be present in the catalyst bed discharge.

[0033] Groups of elements in the table are indicated using the numbering scheme indicated in the version of the periodic table of elements published in Chemical and Engineering News, 63(5), 27, 1985. In some cases, a group of elements may be indicated using a common name assigned to the group; for example, alkali metals for Group 1 elements, alkaline earth metals for Group 2 elements, transition metals for Group 3-12 elements, halogens or halides for Group 17 elements and the like.

[0034] In one aspect, a chemical group can be defined or described according to how that group is formally derived from a reference or precursor compound, for example, by the number of hydrogen atoms removed from the precursor compound to generate the group, even if that group is not literally synthesized in such a way. These groups can be used as substituents or coordinated or bonded to metal atoms. As an example, an alkyl group can formally be derived by removing Petition 870250083407, dated 09 / 16 / 2025, pp. 212 / 309 11 / 91 a hydrogen atom of an alkane. The disclosure that a substituent, ligand, or other chemical moiety may constitute a particular group implies that the well-known rules of chemical structure and bonding are followed when that group is employed as described. When describing a group as being derived from, derived from, formed by, or formed by, such terms are used in a formal sense and are not intended to reflect any specific synthetic methods or procedures unless otherwise specified or the context requires otherwise.

[0035] As used herein, the term hydrocarbon refers to a compound containing only carbon and hydrogen atoms. Other identifiers may be used to indicate the presence of particular groups, if any, in the hydrocarbon. For example, halogenated hydrocarbon indicates the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the hydrocarbon.

[0036] An aromatic compound or aromatic hydrocarbon is a compound containing a cyclically conjugated double bond system that follows Hückel's (4n+2) rule and contains (4n+2) pi-electrons, where n is an integer from 1 to 5. Aromatic hydrocarbons include arenes (aromatic compounds, for example, benzene, toluene, and xylenes) and heteroarenes (heteroaromatic compounds formally derived from arenes by replacing one or more methine carbon atoms (-C=) of the cyclically conjugated double bond system with trivalent or divalent heteroatoms, so as to maintain the continuous pi-electron system characteristic of an aromatic system and a number of out-of-plane pi-electrons corresponding to Hückel's (4n+2) rule).As disclosed in this document, the substituted term may be used to describe an aromatic, arene, or heteroarene group in which a non-hydrogen moiety formally replaces a hydrogen atom in the compound and is intended to be non-limiting unless otherwise specified.

[0037] As used herein, the term alkane refers to a Petition 870250083407, dated 09 / 16 / 2025, pp. 213 / 309 12 / 91 saturated hydrocarbon compound. Other identifiers may be used to indicate the presence of particular groups, if any, in the alkane (for example, halogenated alkane indicates the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the alkane). The term alkyl group is used in this document in accordance with the definition specified by IUPAC: a univalent group formed by the removal of a hydrogen atom from an alkane. The alkane or alkyl group may be linear or branched, unless otherwise specified.

[0038] A cycloalkane is used in this document to refer to a saturated cyclic hydrocarbon, with or without side chains, for example, cyclobutane, cyclopentane, cyclohexane, methylcyclopentane and methylcyclohexane. Other identifiers may be used to indicate the presence of particular groups, if any, in the cycloalkane (for example, halogenated cycloalkane indicates the presence of one or more halogen atoms replacing an equivalent number of hydrogen atoms in the cycloalkane).

[0039] An aliphatic compound or aliphatic hydrocarbon is defined according to the IUPAC recommended definition to mean an acyclic or cyclic carbon compound, saturated or unsaturated, excluding aromatic compounds. That is, an aliphatic compound is a non-aromatic organic compound.

[0040] The term hydrocarbyl group is used in this document in accordance with the definition specified by IUPAC: a univalent group formed by the removal of a hydrogen atom from a hydrocarbon (i.e., a group containing only carbon and hydrogen). Thus, a hydrocarbyl group includes alkyl groups (linear or branched), cycloalkyl groups, alkenyl groups, aryl groups and the like. Non-limiting examples of hydrocarbyl groups include methyl, ethyl, butyl, hexyl, phenyl, tolyl, propenyl and the like.

[0041] As used herein, a paraffin refers to non-cyclic, linear or branched saturated hydrocarbons and includes alkanes. For example, a C6 paraffin is a non-cyclic, linear or Petition 870250083407, dated 09 / 16 / 2025, pages 214 / 309 13 / 91 branched with 6 carbon atoms per molecule. Normal hexane, methylpentanes, and dimethylbutanes are examples of C6 paraffins. A paraffin-containing feed comprises non-cyclic saturated hydrocarbons, such as normal paraffins, isoparaffins, and mixtures thereof.

[0042] As used in this document, naphthenes and naphthenics are terms used to describe saturated cyclic hydrocarbons and include cycloalkanes and their alkyl-substituted analogs. Therefore, a naphthenes is a saturated cyclic hydrocarbon with one or more rings of carbon atoms in its chemical structure and is used in this document to mean the same as a cycloalkane. If such a cyclic structure includes unsaturated carbon-carbon bonds but is not aromatic, such compounds would be aliphatic, but not naphthenic. In some embodiments, a naphthenes are a saturated cyclic hydrocarbon with 5 to 8 carbon atoms in the cyclic structure, including substituted (particularly alkyl-substituted) analogs thereof.

[0043] As used herein, an olefin is an acyclic or cyclic hydrocarbon with one or more carbon-carbon double bonds in addition to those formal in aromatic compounds. Olefins include alkenes, cycloalkenes, and the corresponding polyenes.

[0044] As used herein, naphtha is a petroleum distillate fraction that distills within the range of 50°F (10°C) to 550°F (260°C). In some embodiments, naphtha boils within the range of 70°F (21°C) to 450°F (232°C) and, more typically, within the range of 80°F (27°C) to 400°F (204°C) and often within the range of 90°F (32°C) to 360°F (182°C). In some embodiments, at least 85% by volume (percentage by volume) of naphtha boils within the range of 50°F (10°C) to 550°F (260°C) and, more typically, within the range of 70°F (21°C) to 450°F (232°C). In embodiments, at least 85% by volume of naphtha is in the range of C4 to C12 and, more typically, in the range of C5 to C11 and, often, in the range of C6 to C10. Naphtha may include, for example, direct-run naphthas, refined paraffinic naphthas, and extraction naphthas or Petition 870250083407, dated 09 / 16 / 2025, pp. 215 / 309 14 / 91 aromatic adsorption, C6 to C10 paraffin and feeds containing naphthene, bio-derived naphtha, naphtha from hydrocarbon synthesis processes, including Fischer-Tropsch and methanol synthesis processes, as well as naphtha from other refinery processes, such as hydrocracking or conventional reforming.

[0045] As used herein, the term convertible hydrocarbon, convertible C6 species, or convertible C7 species refers to hydrocarbon compounds that can be selectively converted into aromatic products, such as aromatic hydrocarbons, under flavoring process conditions. In some respects, the feedstream comprises a highly branched hydrocarbon that is not selectively converted into aromatic hydrocarbons under conventional flavoring process conditions. Whereas a highly branched hydrocarbon is a hydrocarbon that is not selectively convertible to form aromatic hydrocarbons under conventional flavoring process conditions.For example, a highly branched hydrocarbon may comprise highly branched hydrocarbons with six or seven carbon atoms with an internal quaternary carbon or hydrocarbons with six carbon atoms and two adjacent internal tertiary carbons or mixtures thereof. Highly branched hydrocarbons may include, but are not limited to, dimethylbutanes (e.g., 2,2-dimethylbutane, 2,3-dimethylbutane), dimethylpentanes (e.g., 2,2-dimethylpentane, 3,3-dimethylpentane), trimethylbutanes (e.g., 2,2,3-trimethylbutane), and mixtures thereof. Highly branched hydrocarbons are not selectively convertible aromatic hydrocarbons and instead convert to light hydrocarbons under aromatization process conditions.The convertible components may comprise methylpentanes, methylhexanes, dimethylpentanes or mixtures thereof and / or the selectively convertible components may comprise at least one of 2-methylpentane, 3-methylpentane, 2,4-dimethylpentane, 2,3-dimethylpentane, n-hexane, 2-methylhexane, 3-methylhexane, n-heptane or mixtures thereof. Petition 870250083407, dated 09 / 16 / 2025, pages 216 / 309 15 / 91 selectively convertible components readily convert to aromatic hydrocarbons without the production of light hydrocarbons.

[0046] As used herein, primary aromatic hydrocarbon, primary aromatic product, desired hydrocarbon product and particular aromatic species are used interchangeably and refer to aromatic hydrocarbons that are the desired end product of the reaction and comprise aromatic hydrocarbons that have been generated from a feed that includes a renewable cellulose source. For example, the desired product may be benzene while toluene and xylenes may be byproducts, or the desired product may be xylenes while benzene and toluene may be byproducts.

[0047] A Group 8-10 metal includes each of the Group 8 metals iron, ruthenium, and osmium, each of the Group 9 metals cobalt, rhodium, and iridium, and each of the Group 10 metals nickel, palladium, and platinum. Group 8-10 metals may also be referred to using the previous nomenclature, Group VIII metals, which also encompasses all iron, ruthenium, osmium, cobalt, rhodium, iridium, nickel, palladium, and platinum. Generally, the description of a catalyst as a Group 8-10 metal catalyst or as comprising a Group 8-10 metal is intended to cover catalysts that include at least one Group 8-10 metal and optionally other metals such as Pt / Sn and Pt / Re.

[0048] The term platinum metal is used in this document to designate the 2nd and 3rd row transition metals of Groups 8-10, namely ruthenium, osmium, rhodium, iridium, palladium and platinum.

[0049] The term noble metal is generally used to describe specific metals that are resistant to corrosion, and this term is used in this document to include certain 2nd and 3rd row transition metals, but no first row transition metals. Generally, noble metals include ruthenium, osmium, rhodium, iridium, palladium, platinum, silver, and gold. Consequently, the noble metals of Group 8-10 are also the platinum metals.

[0050] As used herein, the term linked refers to Petition 870250083407, dated 09 / 16 / 2025, pp. 217 / 309 16 / 91 to describe a combination of zeolite binder or other binder-support combination that is formed into aggregates, such as pellets, pills, extrudates, and the like. The term catalyst base, as used herein, refers to a bonded zeolite or bonded support.

[0051] The term catalyst is used in this document in a broad sense and includes the final catalyst as well as precursors of the final catalyst. Precursors of the final catalyst include, for example, the calcined form of the catalyst containing the catalytic metal and also the catalyst before activation by reduction. The term catalyst is thus used to refer to the activated catalyst in some contexts in this document and in other contexts to refer to precursor forms of the catalyst, as will be understood by those skilled in the art from the context.

[0052] The term sulfur-sensitive describes catalysts that are particularly sensitive to the presence of sulfur in the feedstock. Generally, these catalysts require that the amount of sulfur in the feedstock be reduced to less than 5 ppm by hydrotreatment, adsorbents, or a combination thereof. As used in this document, the terms flavoring reactor system, flavoring reactor unit, catalytic reactor system, and catalytic reactor unit when referring to flavoring reactor systems also refer to the reactor vessel, reactor internals, and associated processing equipment as the context permits, including but not limited to the catalyst, inert packing materials, scallops, flow distributors, central tubes, reactor doors, catalyst transfer and distribution system, furnaces and other heating devices, heat transfer equipment, and piping.The aromatization reactor system described may comprise a fixed catalyst bed system, a moving catalyst bed system, a fluidized catalyst bed system, or combinations thereof. Such aromatization reactor systems may be batch or continuous. In a fixed bed system, the feed flow... Petition 870250083407, dated 09 / 16 / 2025, pages 218 / 309 17 / 91 can flow upwards, downwards, or radially through the reactor. In one aspect, the first catalyst bed, the intermediate catalyst beds, and the last catalyst bed are in a radial flow reactor.

[0053] The term catalyst bed, such as first, second, or intermediate catalyst bed, is used in this document to refer to a specific catalyst composition that constitutes at least a portion or all of the catalyst material in a single flavoring reactor. For example, a first catalyst bed may occupy the entirety of a flavoring reactor, or it may occupy a portion of a flavoring reactor while a second catalyst bed occupies the remaining portion of the flavoring reactor. More typically, each catalyst bed may occupy the entirety of a flavoring reactor. Generally, and unless otherwise specified or the context requires otherwise, multiple flavoring reactors are described as having different catalyst beds, regardless of whether their catalysts have identical or different compositions.

[0054] The term halogen has its usual meaning and, as the context allows, includes halides. Therefore, examples of halogens include fluorine, fluorine, chlorine, chloride, bromine, bromide, iodine, and iodide. Furthermore, the use of the term fluoride and chloride when describing catalyst components or catalyst composition, such as weight percent or molar percent of these components, does not depend on their presence in the catalyst in any particular molecular or ionic form.

[0055] Molar selectivities are defined as follows: Benzene selectivity: $Bz = W-Bz,prod Eq. 1 W-conv C6,feed ^-conv C6,prod W-TOL,Prod $Tol = Toluene selectivity: Eq. 2 W-conv C7,feed ^-conv C7,prod Benzene selectivity + $Bz+Tol = ^Bzprod + ^TOLfrod Eq. 3 Toluene: W-conv C6,C7,feed ^-conv C6,C7,prod Petition 870250083407, dated 09 / 16 / 2025, pages 219 / 309 18 / 91 Selectivity of aromatics: ç, _ '^Bz,prod + ^TOLProd + ^-C8+ arom,prodSarom= * T~— . - -r, ~~~7. :Eq 4nconv C6-C8+,alimentação,Lconv C6-C8+,prod

[0056] Conversion is defined as the number of moles converted per mole of convertible hydrocarbons fed as follows: Conversion C6: W-conv C6,feed ^-conv C6,prod _ _ xc6 = . Eq. 5 nconv C6,feed Conversion C7: „ W-conv C7,feed ^-conv C7,prod Xc7 = . Eq. 6 'iconv C7,feed Conversion C6+ XC6+C7 C7: _ fi-conv C6,feed + ^-conv C7,feed ^-conv C6,prod ^-conv C7,prod Eq. 7 W-conv C6,feed + ^conv C7,feed

[0057] In these equations, n indicates a molar flow rate in a continuous reactor or the number of moles in a batch reactor.

[0058] A ton is used in this document to refer to a metric ton, that is, a unit of mass equal to 1,000 kilograms.

[0059] The Summary of this application is not intended to be used to interpret the scope of the claims or to limit the scope of the matter disclosed herein, but rather to satisfy the requirements of 37 CFR § 1.72(b), to enable the United States Patent and Trademark Office and the general public to quickly determine from a cursory inspection the nature and substance of the technical disclosure. Furthermore, any headings employed herein are also not intended to be used to interpret the scope of the claims or to limit the scope of the matter disclosed herein. Any use of the past tense to describe any example otherwise indicated as constructive or prophetic is not intended to reflect that the constructive or prophetic example was actually realized.

[0060] All publications and patents mentioned in this document are incorporated herein by reference in their entirety for the purpose of describing and disclosing, for example, the constructs and methodologies that are described in the publications, which may be used in connection with the invention presently described. The publications discussed herein Petition 870250083407, dated 09 / 16 / 2025, pp. 220 / 309 19 / 91 throughout the text are provided only for your disclosure prior to the filing date of this application. Nothing in this document should be construed as an admission that the inventors do not have the right to anticipate such disclosure by virtue of the prior invention.

[0061] Those skilled in the art will readily appreciate that many modifications are possible in the exemplary embodiments disclosed in this document without materially departing from the new teachings and advantages according to this disclosure. Consequently, all such modifications and equivalents are intended to be included within the scope of this disclosure, as defined in the following claims. Therefore, it should be understood that recourse may be made to various other aspects, embodiments, modifications, and equivalents thereof which, after reading the description in this document, may suggest themselves to one skilled in the art without departing from the spirit of the present disclosure or the scope of the appended claims. DETAILED DESCRIPTION

[0062] This disclosure is generally directed to methods for regenerating and / or reactivating spent catalysts, such as spent aromatization catalysts. It has been unexpectedly discovered that, by using a fluorine-containing compound instead of fluorine gas during a fluorination step, the methods in this document can achieve an improved distribution of fluorine throughout a catalyst bed, with little or no impact on the performance of the regenerated and / or reactivated catalysts.

[0063] Any spent catalyst can be subjected to the methods described herein. In some embodiments, a spent catalyst includes a transition metal and a catalyst support. A catalyst, such as a spent catalyst, may be present in a metal reactor during some or all of the steps of the methods provided herein. In some embodiments, the metal reactor includes stainless steel, for example, 347SS or 321SS. Methods

[0064] The reform methods are provided in this document, Petition 870250083407, dated 09 / 16 / 2025, pp. 221 / 309 20 / 91 which may include any two or more (such as any two, any three, any four, any five, any six, any seven, or all eight) of the following steps: (A) contacting a hydrocarbon feed with an aromatization catalyst including a transition metal and a catalyst carrier under reforming conditions in a metal reactor system to produce an aromatic product; (B) carrying out step (A) for a period of time sufficient to form a spent catalyst; (C) contacting the spent catalyst with hydrogen gas to produce a removed spent catalyst; (D) subjecting the removed spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding about 500°F, for a time effective to remove from the spent catalyst at least a portion of the hydrogen carbon feed, at least a portion of the aromatic product, or a combination thereof to form a treated spent catalyst;(E) contacting the treated spent catalyst with a chlorine-containing stream including a chlorine-containing compound to produce a chlorinated spent catalyst; (F) subjecting the chlorinated spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding 900°F, for a time effective to improve a dispersion of the transition metal in the chlorinated spent catalyst to form a redistributed spent catalyst; (G) contacting the redistributed spent catalyst with a fluorine-containing stream comprising a fluorine-containing compound to form a regenerated catalyst;and (H) reduce the regenerated catalyst. The methods herein may also include a catalyst reactivation step, such as after step (H). In some embodiments, the reforming methods in this document are in situ processes. Therefore, in some embodiments, steps (A)-(H) (or two or more of the (A)-(H) steps that are selected) are carried out in the same reactor system. In some embodiments, steps (C)-(H) are carried out externally to a reactor system in which steps (A)-(B) are carried out. For example, steps (C)-(H) may be carried out in a metal reactor that is not in the reforming reactor system. Petition 870250083407, dated 09 / 16 / 2025, pp. 222 / 309 21 / 91

[0065] In some embodiments, the methods include (1) contacting the spent catalyst with hydrogen gas to produce a removed spent catalyst; (2) subjecting the removed spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding about 500°F, for a time effective to remove from the spent catalyst at least a portion of the carbon hydrogen feed, at least a portion of the aromatic product, or a combination thereof to form a treated spent catalyst; (3) contacting the treated spent catalyst with a chlorine-containing stream including a chlorine-containing compound to produce a chlorinated spent catalyst; (4) subjecting the chlorinated spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding 900°F, for a time effective to improve a dispersion of the transition metal in the chlorinated spent catalyst to form a redistributed spent catalyst;(5) contacting the spent redistributed catalyst with a fluorine-containing stream including a fluorine-containing compound to form a regenerated catalyst; and (6) reducing the regenerated catalyst.

[0066] In some embodiments, the methods include (A) contacting a hydrocarbon feed with an aromatization catalyst including a transition metal and a catalyst carrier under reforming conditions in a metal reactor system to produce an aromatic product; (B) carrying out step (A) for a period of time sufficient to form a spent catalyst; (C) contacting the spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst, wherein, optionally, the chlorine-containing compound comprises chlorine, a chlorinated hydrocarbon, a chlorofluorocarbon (CFC), a chlorofluorocarbon (HCFC), or a combination thereof; (D) contacting the chlorinated spent catalyst with a decoking gas stream comprising oxygen to produce a non-coking catalyst;and (E) contacting the uncoking catalyst with a fluorine-containing stream including a fluorine-containing compound, wherein the fluorine-containing compound includes; Petition 870250083407, dated 09 / 16 / 2025, pp. 223 / 309 22 / 91 a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a chlorofluorocarbon (HCFC), a fluorocarbon (FC), or a combination thereof. In some embodiments, the methods are in situ processes. For example, steps (A)-(E) may be carried out in the same reactor system. In some embodiments, steps (C)-(E) are carried out externally to the reactor system of steps (A)-(B). For example, steps (C)-(E) may be carried out in a metal reactor that is not in the reforming reactor system. In some embodiments, the methods include reactivating the catalyst after step (E).

[0067] In some embodiments, the methods include regenerating a spent catalyst comprising a transition metal and a catalyst support in a metal reactor. The methods may include (1) contacting the spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst; (2) contacting the chlorinated spent catalyst with a decoking gas stream comprising oxygen to produce a decoking catalyst; and (3) contacting the decoking catalyst with a fluorine-containing stream comprising a fluorine-containing compound to produce a regenerated catalyst, wherein the fluorine-containing compound includes a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a chlorofluorocarbon (HCFC), a fluorocarbon (FC), or a combination thereof.

[0068] The steps of the methods provided in this document can generally be performed in any effective time period, temperature, pressure, etc. Hydrogen Gas

[0069] Contact of a spent catalyst with hydrogen gas can occur at any effective temperature. In some embodiments, contact of a spent catalyst with hydrogen gas occurs, at least in part, at a temperature above 25°F, above 100°F, above 200°F, above 300°F, above 400°F, or above 500°F. In some embodiments, the Petition 870250083407, dated 09 / 16 / 2025, pp. 224 / 309 23 / 91 Contact of a spent catalyst with hydrogen gas occurs, at least in part, at a temperature of about 300°F to about 800°F, about 400°F to about 800°F, or about 500°F to about 800°F.

[0070] The contact of a spent catalyst with hydrogen can occur for any effective time. In some embodiments, the contact of a spent catalyst with hydrogen gas occurs for a time of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours, or about 1 minute to about 2 hours. Compounds and streams containing fluorine

[0071] The fluorine-containing compounds used in the methods described herein may include any compound, in any phase, that includes in its structure one or more fluorine atoms. For example, a fluorine-containing compound may include a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC), a fluorocarbon (FC), or a combination thereof. In some embodiments, the fluorine-containing compound is a compound of formula (I) CaHbClcFd Formula (I),

[0072] wherein a is 1 to 6, b is 0 to 14, c is 0 to 14, d is 1 to 14, wherein, optionally, b and / or c is not 0, wherein b + c + d = 2a + 2, and wherein, optionally, the compound of formula (I) is substituted. In some embodiments, the fluorine-containing compound is 1,1,1,2-tetrafluoroethane. In some embodiments, the fluorine-containing compound is difluoromethane. In some embodiments, the fluorine-containing compound is dichlorodifluoromethane.

[0073] Fluorine-containing compounds may be a component of a fluorine-containing chain. A fluorine-containing chain may consist of one or more fluorine-containing compounds, such as one, two, three, etc. fluorine-containing compounds. A fluorine-containing chain may include at least one component other than one or more fluorine-containing compounds. The at least one component other than one or more fluorine-containing compounds may be a Petition 870250083407, dated 09 / 16 / 2025, pages 225 / 309 24 / 91 fluid, such as an inert gas, air, oxygen gas, etc. In some embodiments, the fluorine-containing stream includes (i) a fluorine-containing compound and any inert gas disclosed in this document, for example, nitrogen, (ii) a fluorine-containing compound, any inert gas disclosed in this document and air, (iii) a fluorine-containing compound and air, or (iv) a fluorine-containing compound, oxygen (O2) and any inert gas disclosed in this document, for example, nitrogen.

[0074] One or more fluorine-containing compounds may be present in a fluorine-containing stream in any concentration and / or ratio. When two or more components other than the fluorine-containing compound(s) are present in a fluorine-containing stream, the two or more components may be present in any concentration and / or ratio (volume ratio or weight ratio). For example, a fluorine-containing stream may include an inert gas and air, and the inert gas and air may be present in a volume ratio of about 3:1 to about 30:1, about 3:1 to about 20:1, about 3:1 to about 10:1, about 3:1 to about 5:1, or about 4:1. As a further example, a volume ratio of an inert gas to oxygen (O2) in a fluorine-containing stream can be from about 90:10 to about 99.9:0.1, from about 95:5 to about 99:1, or about 97:3 (inert gas: oxygen (O2)).In some embodiments, a fluorine-containing current includes from about 0.01 mol% to about 40 mol%, from about 0.01 mol% to about 30 mol%, from about 0.01 mol% to about 20 mol%, from about 0.01 mol% to about 10 mol%, or from about 0.01 mol% to about 5 mol% of oxygen. Oxygen (O2) can be a component of air.

[0075] A fluorine-containing stream can be formed with the aid of any known equipment, and the components of a fluorine-containing stream can be combined in any manner and / or order, such as simultaneously, sequentially, etc. In some embodiments, the contact of a spent redistributed catalyst with a fluorine-containing stream includes the circulation of a fluid, such as an inert gas, and the injection of a fluorine-containing compound into the circulating fluid. In some embodiments, the injection of a Petition 870250083407, dated 09 / 16 / 2025, pp. 226 / 309 25 / 91 The fluorine-containing compound is achieved, at least in part, with a spray apparatus, such as a spray apparatus configured to disperse the fluorine-containing compound in a circulating fluid, such as an inert gas, oxygen, or a combination thereof. For example, contacting a spent redistributed catalyst with a fluorine-containing stream may involve circulating a stream that includes an inert gas and oxygen (O2) and injecting the fluorine-containing compound into the circulating stream. A circulating stream may include oxygen (O2) at any concentration. In some modes, oxygen (O2) is present in a circulating stream at a concentration of about 0.01% to about 10%, about 0.01% to about 8%, about 0.01% to about 6%, about 0.01% to about 4%, about 1% to about 4%, about 2% to about 4%, about 2.5% to about 3.5%, or about 3%, by volume.

[0076] A catalyst, such as a spent redistributed catalyst, may be brought into contact with a fluorine-containing compound or a fluorine-containing stream in any manner and under any conditions effective to bring into the catalyst a desired percentage by weight of fluorine, such as a percentage by weight of up to 3%, up to 2% or up to 1%.

[0077] In some embodiments, the contact of a spent catalyst, such as redistributed spent catalyst, with a fluorine-containing stream includes (a) providing two or more reactors in fluid communication with each other, wherein the two or more reactors are connected in a series, thus enabling a fluorine-containing stream to be (i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to one of the first two or more reactors and, optionally, (iv) sequentially recirculated through each of the two or more reactors, wherein each of the two or more reactors includes a reservoir in which the spent catalyst is disposed; (b) heating one of the two or more reactors to a temperature that is equal to or greater than a fluorination temperature and maintaining Petition 870250083407, dated 09 / 16 / 2025, pp. 227 / 309 26 / 91 each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature, where the fluorination temperature is effective to decompose at least partially a fluorinated compound from the fluorinated stream; and (c) inject the fluorinated stream and circulate or recirculate the fluorinated stream for an effective time to achieve a desired level of fluorination of the spent catalyst in one of the two or more reactors at a temperature that is equal to or higher than the fluorination temperature.

[0078] When the systems and methods in this document include a group of components, such as reactors, that are connected in a series, the component arbitrarily referred to as the first is the component that is furthest upstream, and the remaining components are numbered sequentially thereafter, with the highest number arbitrarily assigned to the component that is downstream of all other components in the group. For example, if a system includes three reactors, the first reactor is upstream of the second and third reactors, and the third reactor is downstream of the first and second reactors. Therefore, if a limitation in this document states that a stream is returned to one of the first two or more reactors, then this limitation indicates that the stream is passed to the reactor that is upstream of the other two or more reactors.

[0079] The methods may also include heating one of the two or more reactors to a temperature that is equal to or greater than the fluorination temperature and maintaining each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature; and injecting the fluorinated stream and circulating or recirculating the fluorinated stream for an effective time to achieve a desired level of fluorination of the spent catalyst in the different two or more reactors at a temperature that is equal to or greater than the fluorination temperature. These elements may be repeated until the spent catalyst in each of the one or more reactors is fluorinated to the desired level.

[0080] A stream containing fluorine can be flowed once Petition 870250083407, dated 09 / 16 / 2025, pp. 228 / 309 27 / 91 through the two or more reactors, or the fluorine-containing stream can be recirculated any number of times through the two or more reactors. Recirculation can continue until a desired concentration of fluorine is placed in the catalyst.

[0081] A fluorination temperature may include any temperature at which a fluorine-containing compound decomposes at least partially. In some embodiments, the temperature that is equal to or greater than the fluorination temperature is at least 700 °F. In some embodiments, the temperature that is equal to or greater than the fluorination temperature is about 650 °F to about 850 °F, about 700 °F to about 850 °F, about 700 °F to about 800 °F, about 700 °F to about 775 °F, or about 700 °F to about 750 °F. In some embodiments, the temperature that is less than the fluorination temperature is about 600 °F or less. In some embodiments, the temperature that is below the fluorination temperature is about 300°F to about 600°F, about 400°F to about 600°F, or about 500°F to about 600°F.

[0082] A fluoride-containing stream may be introduced into two or more reactors in any manner. In some embodiments, a fluoride-containing stream is injected. Injection of the fluoride-containing stream may include (1) selecting an injection point from one or more injection points and (2) injecting the fluoride-containing stream into the selected injection junction from one or more injection points. The selected injection point may be any of those present in the systems provided in this document. In some embodiments, the selected injection point is (i) upstream of a reactor (or the different reactor) heated to a temperature that is equal to or greater than the fluorination temperature, (ii) downstream of all other reactors upstream of the reactor (or the different reactor) heated to a temperature that is equal to or greater than the fluorination temperature, or (iii) a combination thereof.

[0083] The amount of fluoride-containing compound or fluoride-containing stream that is injected and circulated / recirculated can be effective in placing Petition 870250083407, dated 09 / 16 / 2025, pages 229 / 309 28 / 91 in spent catalyst any amount of fluorine, such as about 0.1% by weight to about 1.5% by weight of fluorine, about 0.5% by weight to about 1.5% by weight of fluorine, or about 0.15% by weight to about 1.2% by weight of fluorine. Methods may include analyzing the fluorine-containing stream during circulation or recirculation of the fluorine-containing stream to determine an amount or concentration of the fluorine-containing compound and / or fluorine in the fluorine-containing stream. Methods may include stopping the circulation / recirculation of the fluorine-containing stream when the amount or concentration of the fluorine-containing compound and / or fluorine is equal to or less than a threshold concentration or amount that indicates successful fluorine deposition in spent catalyst. Monitoring of the fluorine-containing stream can be achieved using any known technique or apparatus, such as spectroscopy.

[0084] Systems for fluoridating a spent catalyst are also provided in this document. The systems may include (a) two or more reactors in fluid communication with each other, wherein the two or more reactors are connected in a series, thus allowing a fluid stream, such as a stream containing fluorine, to be (i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to a first of the two or more reactors and, optionally, (iv) sequentially recirculated through each of the two or more reactors; and (b) two or more heating devices configured to heat each of the two or more reactors to the same or different temperatures.

[0085] One embodiment of a system is represented in FIG. 1. System 100 includes a first furnace 110 configured to heat a first reactor 120, a second furnace 111 configured to heat a second reactor 121, and a third furnace 112 configured to heat a third reactor 122, wherein these components are connected in series via piping 101, which includes a feedback circuit 102 that allows a circulating current to be recirculated from the third reactor 122 to the first reactor 110. Petition 870250083407, dated 09 / 16 / 2025, pages 230 / 309 29 / 91 Although three reactor / furnace pairs (110 / 120, 111 / 121, 112 / 122) are shown in FIG. 1, systems may include two, three, four, five, six, seven, eight, nine, ten or more reactors. System 100 in FIG. 1 includes three possible injection points (130, 131, 132), which are upstream of the first reactor 120, the second reactor 121 and the third reactor 122, respectively. Furnaces with configurations different from those shown in FIG. 1 may be used, such as tube furnaces or others.

[0086] System 100 of FIG. 1 can be used to carry out embodiments of the methods provided in this document. For example, in some embodiments, the methods include (i) heating reactor 120 with furnace 110 to a temperature of about 700°F to about 850°F, (ii) maintaining the temperatures of the second reactor 121 and the third reactor 122 at or below about 600°F, (iii) injecting a fluorine-containing stream at the first injection point 130 and circulating or recirculating the fluorine-containing stream through the first 120, second 121 and third 122 reactors for an effective time to deposit a desired level of fluorine on the spent catalyst 140 of the first reactor 120.The methods may also include (i) reducing the temperature of the first reactor 120 to a temperature of about 600°F or less, (ii) using furnace 111 to increase the temperature of the second reactor 121 to a temperature of about 700°F to about 850°F, (iii) maintaining the temperatures of the first reactor 120 and the third reactor 122 at or below about 600°F, and (iv) injecting a fluorine-containing stream at the second injection point 131 and circulating or recirculating the fluorine-containing stream through the second 121, third 122, and first 120 reactors for an effective time to deposit a desired level of fluorine on the spent catalyst 141 of the second reactor 121.The methods may also include (i) reducing the temperature of the second reactor 121 to a temperature of about 600°F or less, (ii) using furnace 112 to increase the temperature of the third reactor 122 to a temperature of about 700°F to about 850°F, (iii) maintaining the temperatures of the first reactor 120 and the second reactor 121 at or below about 600°F, and (iv) injecting a fluorine-containing stream at the third point. Petition 870250083407, dated 09 / 16 / 2025, pp. 231 / 309 30 / 91 injection 132e circulate or recirculate the fluorine-containing stream through the third 122, first 120 and second 121 reactors for an effective time to deposit a desired level of fluorine on the spent catalyst 142 of the second reactor 122.

[0087] In some embodiments, (i) an amount of fluorine-containing compound in a fluorine-containing stream, (ii) a duration of contact of the spent catalyst with the fluorine-containing stream, or (iii) a combination thereof is selected to place in the spent catalyst redistributed about 0.1% by weight to about 2% by weight, about 0.15% by weight to about 1.5% by weight, about 0.2% by weight to about 1.5% by weight, about 0.2% by weight to about 1% by weight, about 0.5% by weight to about 1.5% by weight, about 0.5% by weight to about 1% by weight, or about 0.8% by weight to about 1% by weight of fluorine. In some embodiments, the contact of a catalyst, such as a spent catalyst, and the fluorine-containing stream occurs, at least partially, at a temperature of about 500°F to about 1,000°F, about 600°F to about 1,000°F, about 600°F to about 900°F, about 700°F to about 900°F, or about 700°F to about 850°F. In some embodiments,The amount of fluorine-containing compound in the fluorine-containing stream is controlled to give a desired concentration of fluorine [F] in the catalyst, such as a concentration lower than any maximum amount or within any range disclosed in this document, for example, less than about 10% by weight, less than about 8% by weight, less than about 6% by weight, less than about 4% by weight, less than about 2% by weight, less than 1.5% by weight, within a range of about 0.1% by weight to about 3% by weight, about 1% by weight to about 2% by weight, about 1.25% by weight to about 1.75% by weight, about 0.1% by weight to about 1.5% by weight, about 0.15% by weight to about 1.3% by weight, about 0.1% by weight to about 1.0% by weight, about 0.25% by weight to approximately 3% by weight, approximately 0.25% by weight to approximately 2% by weight, approximately 0.25% by weight to approximately 1.75% by weight, approximately 0.25% by weight to approximately 1.5% by weight, approximately 0.25% by weight to approximately 1.3% by weight, approximately 0,25% by weight to approximately 1.0% by, Petition 870250083407, dated 09 / 16 / 2025, pp. 232 / 309 31 / 91 weight, approximately 0.5% by weight to approximately 1% by weight, or approximately 0.3% by weight to approximately 0.8% by weight. In some embodiments, a fluorination step is conducted at (i) a fluorination temperature in any fluorination temperature range disclosed in this document, for example, from about 0°C to about 600°C, from about 10°C to about 550°C, from about 20°C to about 450°C, from about 0°C to about 300°C, from about 20°C to about 250°C, or from about 15°C to about 50°C, (ii) a fluorination pressure of atmospheric pressure to about 15 bar, atmospheric pressure to about 10 bar, atmospheric pressure to about 7 bar, about 2 bar to about 10 bar, about 2 bar to about 5 bar, or about 2 bar.In some embodiments, a fluoridation step is conducted for a period of time within any of the fluoridation time ranges disclosed in this document, for example, from about 0.1 hours to about 96 hours, from about 0.1 hours to about 72 hours, from about 0.1 to about 48 hours, from about 0.1 to about 12 hours, or from about 0.1 to about 8 hours.

[0088] In some embodiments, the amount of fluorine-containing compound in the fluorine-containing stream is controlled to give a concentration of fluorine [F] or a fluorine-containing compound, such as a concentration in a fluorine-containing stream, less than any maximum amount or in any range disclosed in this document, for example, less than about 50,000 ppmv, in a range of about 5 to about 25,000 ppmv, in a range of about 10 to about 25,000 ppmv, in a range of about 50 to about 25,000 ppmv, in a range of about 5,000 to about 25,000 ppmv, in a range of about 50 to about 20,000 ppmv, in a range of about 50 to about 15,000 ppmv, in a range of about 50 to about 10,000 ppmv, in a range of about 50 to about 5,000 ppmv, in a range of about 50 to about 2,500 ppmv, in a range of about 50 to about 1,000 ppmv, in a range of about 500 to about 1.000 ppmv, in a range of about 600 to about 900 ppmv, in a range of about 700 to about 800 ppmv, or about 750 ppmv. Petition 870250083407, dated 09 / 16 / 2025, pp. 233 / 309 32 / 91

[0089] In some embodiments, the concentration of fluorine in the regenerated catalyst is from about 0.15% by weight to about 1.2% by weight, or from about 0.2% by weight to about 1.2% by weight. In some embodiments, the concentration gradient of fluorine in a regenerated catalyst is 60% or less, 50% or less, 40% or less, 30% or less, 20% or less, or 10% or less.

[0090] Generally, a fluorine-containing stream may include any of the compounds, gases, etc. described in this document, and any one or more of the compounds, gases, etc. described in this document may be excluded from a fluorine-containing stream. For example, a fluorine-containing stream may be substantially free of oxygen-containing compounds and / or chlorine-containing compounds that do not include a fluorine atom. A fluorine-containing stream is considered substantially free of a compound when the compound is present in a fluorine-containing stream at a concentration less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw.

[0091] The methods provided in this document may also include recovering at least a portion of the fluoride-containing stream to produce a recovered fluoride-containing stream. Recovery of at least a portion of the fluoride-containing stream may occur after contact of a coke-free catalyst with the fluoride-containing stream. The methods may also include contact of the coke-free catalyst with the recovered fluoride-containing stream. Compounds and streams containing chlorine

[0092] The chlorine-containing compounds used in the methods described herein may include any compound, in any phase, that includes in its structure one or more chlorine atoms. In some embodiments, the chlorine-containing compound includes chlorine gas (Cl2). A chlorine-containing stream may include one or more compounds (e.g., an inert gas) that is not a chlorine-containing compound. In some embodiments, the chlorine-containing stream includes gas Petition 870250083407, dated 09 / 16 / 2025, pp. 234 / 309 33 / 91 chlorine (Cl2) and an inert gas, such as nitrogen (N2). In some embodiments, chlorine-containing compounds include hydrochloric acid, chlorine gas (Cl2), carbon tetrachloride, tetrachloroethylene, chlorobenzene, methyl chloride, methylene chloride, chloroform, allyl chloride, trichloroethylene, a chloramine, a chlorine oxide, a chlorine acid, chlorine dioxide, dichloride monoxide, dichloride hexoxide, chloric acid, perchloric acid, ammonium chloride, tetramethylammonium chloride, tetraethylammonium chloride, tetrapropylammonium chloride, tetrabutylammonium chloride, methyltriethylammonium chloride, or any combination thereof.

[0093] A chlorine-containing stream can be formed with the aid of any known equipment, and the components of a chlorine-containing stream can be combined in any manner and / or order, such as simultaneously, sequentially, etc. For example, the methods in this document may include circulating a fluid, such as an inert gas, and injecting a chlorine-containing compound into the circulating fluid. The injection of a chlorine-containing compound can be achieved, at least in part, with a spray apparatus configured to disperse the chlorine-containing compound in the circulating inert gas.

[0094] In some embodiments, the amount of chlorine-containing compound in the chlorine-containing stream is controlled to give a desired concentration of chlorine (Cl) or chlorine-containing compound, such as less than any maximum amount or within any range disclosed in this document, for example, less than about 50,000 ppmv, in a range of about 5 to about 25,000 ppmv, in a range of about 10 to about 25,000 ppmv, in a range of about 50 to about 25,000 ppmv, in a range of about 50 to about 20,000 ppmv, in a range of about 50 to about 15,000 ppmv, in a range of about 50 to about 10,000 ppmv, in a range of about 50 to about 5,000 ppmv, in a range of about 50 to about 2,500 ppmv, in a range of about 50 to about 1,000 ppmv, in a range of about 50 to about 500 ppmv, in a range Petition 870250083407, dated 09 / 16 / 2025, pages 235 / 309 34 / 91 from about 50 to about 100 ppmv, in a range of about 100 to about 750 ppmv, or in a range of 500 to about 600 ppmv.

[0095] A catalyst may be brought into contact with a chlorine-containing compound or a chlorine-containing stream in any manner and under any conditions effective to place on the catalyst a desired percentage by weight of chlorine or the chlorine-containing compound, such as a percentage by weight of up to 3%, up to 2%, or up to 1%. In some embodiments, (i) the amount of chlorine-containing compound in the chlorine-containing stream, (ii) the duration of contact of the treated spent catalyst and the chlorine-containing stream, or (iii) a combination thereof is controlled to place on the treated spent catalyst about 0.1% by weight to about 2% by weight, about 0.5% by weight to about 1.5% by weight, about 0.5% by weight to about 1% by weight, or 0.6% by weight to about 1% by weight of chlorine or the chlorine-containing compound.

[0096] Generally, a chlorine-containing stream may include any of the compounds, gases, etc. described in this document, and any one or more of the compounds, gases, etc. described in this document may be excluded from a chlorine-containing stream. For example, a chlorine-containing stream may be substantially free of oxygen-containing compounds and / or fluorine-containing compounds. A chlorine-containing stream is considered substantially free of a compound when the compound is present in a chlorine-containing stream at a concentration less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw.

[0097] A catalyst may be brought into contact with a chlorine-containing compound or chlorine-containing stream in any manner and under any conditions (e.g., temperature, pressure, etc.). In some embodiments, the chlorination step is conducted at a chlorination temperature in any of the chlorination temperature ranges disclosed in this document, for example, from about 0°F to about 600°F, from about 100°F to about 600°F, from about 200°F to about 600°F, from about 300°F to about 600°F, from about Petition 870250083407, dated 09 / 16 / 2025, pp. 236 / 309 35 / 91 approximately 400°F to approximately 600°F, approximately 400°F to approximately 500°F, or approximately 400°F to approximately 450°F. In some embodiments, the chlorination step is conducted for a period of time in any range of chlorination time periods disclosed in this document, for example, from approximately 0.5 hours to approximately 72 hours, from approximately 0.75 hours to approximately 60 hours, from approximately 1 hour to approximately 48 hours, from approximately 1 hour to approximately 12 hours, or from approximately 2 hours to approximately 8 hours. In some embodiments, the chlorination step is conducted at a chlorination temperature of about 0°F to about 600°F, about 100°F to about 600°F, about 200°F to about 600°F, about 300°F to about 600°F, about 300°F to about 500°F, about 350°F to about 500°F, or about 350°F to about 450°F.In some embodiments, the chlorination step is conducted for a period of time within any of the chlorination time ranges disclosed in this document, for example, from about 0.10 hours to about 72 hours, from about 0.50 hours to about 60 hours, from about 0.5 to about 48 hours, from about 0.5 to about 12 hours, or from about 1 to about 8 hours. Gas Stream Decoction

[0098] A decoking gas stream may include any of those known in the art. In some embodiments, a decoking gas stream includes any combination of an inert gas (one or more) and oxygen disclosed in this document, for example, a mixture of nitrogen and oxygen, air, or a mixture of air and nitrogen.

[0099] The oxygen concentration in a decoking gas stream may be limited. In some embodiments, a decoking gas stream includes a molar percentage of oxygen less than any maximum amount or in any range disclosed in this document, for example, less than about 5 molar percent, in a range of about 0.1 to about 10 molar percent, in a range of about 0.1 to about 8 molar percent, in a range of about 0.1 to about 5 molar percent, in a range of about 0.5 to about 3 molar percent, or in a range of about 0.5 to about 6 molar percent. Petition 870250083407, dated 09 / 16 / 2025, pp. 237 / 309 36 / 91

[0100] A decoking gas stream may include any one or more of the compounds disclosed in this document, or any one or more of the compounds disclosed in this document may be excluded from a decoking gas stream. In some embodiments, a decoking gas stream is substantially free of halogen-containing compounds, such as added halogen-containing compounds (e.g., substantially halogen-free, substantially chlorine-free). A decoking gas stream is substantially free of a halogen-containing compound when the halogen-containing compound is present at a concentration less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw. In some embodiments, a decoking gas stream is substantially free of water (e.g., added water).A decoking gas stream is substantially free of water when water is present at a concentration of less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw. Carbon Burning

[0101] The carbon burning steps of the methods provided in this document can be conducted under any effective conditions (e.g., temperature, time, etc.). In some embodiments, the carbon burn-off temperature of a catalyst, such as a spent, removed catalyst, is about 300°F to about 600°F, about 350°F to about 550°F, about 350°F to about 500°F, about 400°F to about 475°F. In some embodiments, the carbon burn-off temperature of a catalyst, such as a spent chlorinated catalyst, is about 500°F to about 1200°F, about 500°F to about 1100°F, about 500°F to about 1000°F, about 600°F to about 1000°F, about 700°F to about 1000°F, about 700°F to about 900°F, about 800°F. F at approximately 900°F or approximately 850°F. In some embodiments, a carbon burning step is conducted at a peak decoking temperature in any peak temperature range of Petition 870250083407, dated 09 / 16 / 2025, pp. 238 / 309 37 / 91 decoking disclosed herein, for example, from about 100°C (about 212°F) to about 700°C (about 1,292°F), from about 125°C (about 257°F) to about 650°C (about 1,202°F), from about 150°C (302°F) to about 600°C (about 1,112°F), from about 200°C (about 392°F) to about 500°C (about 932°F), or from about 350°C (about 662°F) to about 450°C (about 842°F). In some embodiments, a carbon burning step is initiated at an initial decoking temperature that is the same as any chlorine purge temperature disclosed in this document, for example, from about 0°C (about 32°F) to about 300°C (about 572°F), from about 20°C (about 68°F) to about 275°C (about 527°F), from about 20°C (about 68°F) to about 250°C (about 482°F), or from about 50°C (about 122°F) to about 200°C (about 392°F).

[0102] The carbon burn-off of the removed spent catalyst can occur over a period of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours, or about 1 minute to about 2 hours. In some embodiments, the carbon burn-off of a catalyst, such as a spent chlorinated catalyst, occurs over a period of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours, or about 1 minute to about 2 hours.In some embodiments, the carbon burning stage is conducted for a period of time within any range of decoking time periods disclosed in this document, for example, from about 0.5 hours to about 120 hours, from about 0.75 hours to about 108 hours, from about 1 hour to about 96 hours, from about 1 hour to about 72 hours, from about 12 hours to about 48 hours, or from about 1 hour to about 6 hours.

[0103] A carbon burn-off step can remove any desired amount of hydrocarbon feed and / or aromatic feed from a catalyst. For example, carbon burn-off of a catalyst, such as a spent catalyst removal, can remove from Petition 870250083407, dated 09 / 16 / 2025, pp. 239 / 309 38 / 91 spent catalyst at least 90% by weight, at least 95% by weight, at least 99% by weight or 100% by weight of the hydrocarbon feed. Carbon burning of a catalyst, such as a spent catalyst, can remove at least 90% by weight, at least 95% by weight, at least 99% by weight or 100% by weight of an aromatic product from the spent catalyst. A quantity of soft coke may be absorbed and / or adsorbed onto a catalyst, such as a spent catalyst, and carbon burning of the catalyst may reduce the amount of soft coke absorbed and / or adsorbed onto the spent catalyst.In some embodiments, the carbon burning step is conducted for a period of time sufficient to reduce the % by weight of carbon in a catalyst, such as a spent chlorinated catalyst, to less than any maximum % by weight of carbon disclosed herein, for example, less than about 1% by weight, less than about 0.5% by weight, or less than about 0.2% by weight.

[0104] A carbon burn-off of a catalyst, such as a chlorinated catalyst, can improve the dispersion of the transition metal in the catalyst. For example, a carbon burn-off can improve the dispersion of a group VIII metal in the catalyst by at least 40%, at least 50%, at least 60%, at least 70%, at least 80%, or at least 90%. Partial Decoction Stage

[0105] The methods provided in this document may include a partial decoking step. The partial decoking step may be conducted at any effective point in a method, such as before a chlorination step. A partial decoking step may include contacting a catalyst, such as a spent catalyst, with a partial decoking gas stream, which may include oxygen.

[0106] The partial decoking gas stream may include any combination of an inert gas (one or more) and oxygen disclosed in this document, for example, a mixture of nitrogen and oxygen or air. The partial decoking gas stream may include a lower molar % of oxygen. Petition 870250083407, dated 09 / 16 / 2025, pages 240 / 309 39 / 91 that any maximum quantity or any range disclosed in this document, for example, less than about 5% molar, or in a range of about 0.1 to about 4% molar, about 0.1 to about 3% molar, about 0.5 to about 3% molar, or about 1 to about 3% molar.

[0107] A partial decoking gas stream may include any of the compounds disclosed in this document, and any of the compounds disclosed in this document may be excluded from a partial decoking gas stream. For example, a partial decoking gas stream may be substantially free of halogen-containing compounds (e.g., substantially halogen-free). A partial decoking gas stream is substantially free of halogen-containing compounds when halogen-containing compounds are present at a concentration less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw. As a further example, the decoking gas stream may be substantially free of water. A decoking gas stream is substantially free of water when water is present at a concentration less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw.

[0108] A partial decoking step can be conducted under any effective conditions (e.g., time, temperature, etc.). A partial decoking step can be conducted at a partial decoking temperature in any of the partial decoking temperature ranges disclosed in this document, for example, from about 150°C (about 302°F) to about 600°C (about 1112°F), from about 150°C (about 302°F) to about 250°C (about 482°F). A partial decoking step can be conducted for a period of time in any of the partial decoking time ranges disclosed in this document, for example, from about 1 hour to about 48 hours, or from about 2 to about 24 hours. A partial decoking step can be conducted for a period of time sufficient to reduce the % by weight of carbon in the spent catalyst to any range. Petition 870250083407, dated 09 / 16 / 2025, pp. 241 / 309 40 / 91 percentage by weight of carbon disclosed in this document, for example, from about 0.05% by weight to about 10% by weight, from about 0.1% by weight to about 10% by weight, from about 0.05% by weight to about 5% by weight, from about 0.1% by weight to about 5% by weight, from about 1% by weight to 10% by weight, or from about 4% by weight to about 5% by weight. Pre-drying steps

[0109] The methods provided in this document may include a pre-drying step. A pre-drying step may be performed at any effective point in a process. In some embodiments, the methods include performing a pre-drying step before a chlorination step.

[0110] A pre-drying step may include contacting a spent catalyst with a pre-drying gas stream. A pre-drying gas stream may include any inert gas disclosed in this document, for example, nitrogen. A pre-drying gas stream may include any of the compounds disclosed in this document, and any of the compounds disclosed in this document may be excluded from a pre-drying gas. For example, a pre-drying gas stream may be substantially free of oxygen-containing compounds. A pre-drying gas stream is substantially free of oxygen-containing compounds when oxygen-containing compounds are present at a concentration of less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw.

[0111] A pre-drying step can be carried out under any effective conditions (e.g., time, temperature, pressure, etc.). A pre-drying step can be conducted at a pre-drying temperature in any pre-drying temperature range disclosed in this document, for example, from about 75°C to about 500°C, from about 100°C to about 500°C, from about 0°C to about 400°C, from about 100°C to about 400°C, from about 125°C to about 300°C, or from about 180°C to about Petition 870250083407, dated 09 / 16 / 2025, pp. 242 / 309 41 / 91 of 280°C. A pre-drying step may be conducted for a period of time in any range of pre-drying time periods disclosed in this document, for example, from about 1 hour to about 96 hours, or from about 1 hour to about 48 hours. In some embodiments, a pre-drying step is conducted for a period of time sufficient to reduce the moisture content of a catalyst, such as a spent catalyst, to a desirable extent, such as to a concentration lower than any maximum moisture content of a spent catalyst disclosed in this document, for example, lower than about 4% by weight, or lower than about 1% by weight. Chlorine purge stage

[0112] The methods provided in this document may include a chlorine purge step. A chlorine purge step may be performed at any point in the methods provided here, such as before a carbon burning step.

[0113] A chlorine purge step may include contact of a catalyst, such as a spent chlorinated catalyst, with a chlorine purge stream. A chlorine purge stream may include any inert gas disclosed in this document, for example, nitrogen. A chlorine purge stream may include any of the compounds disclosed in this document, and any of the compounds disclosed in this document may be excluded from a chlorine purge stream. For example, a chlorine purge stream may be substantially free of oxygen-containing compounds, for example, oxygen-containing compounds are present in concentrations less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw.As a further example, a chlorine purge stream may be substantially free of halogen-containing compounds (substantially halogen-free), for example, halogen-containing compounds are present in concentrations below about 100 ppmw, below about 50 ppmw, or below about 25 ppmw.

[0114] A chlorine purge step can be carried out under Petition 870250083407, dated 09 / 16 / 2025, pp. 243 / 309 42 / 91 any effective conditions (e.g., time, temperature, pressure, etc.). In some embodiments, a chlorine purge step is conducted at a chlorine purge temperature in any of the chlorine purge temperature ranges disclosed in this document, for example, from about 0°C to about 400°C, from about 15°C to about 350°C, from about 15°C to about 300°C, or from about 25°C to about 250°C. A chlorine purge step may be conducted for a period of time in any of the chlorine purge time ranges disclosed in this document, for example, from about 1 hour to about 96 hours, from about 1 hour to about 48 hours.A chlorine purge step may be conducted for a period of time sufficient to reduce the chlorine content of the outgoing chlorine purge effluent stream, after contact with a catalyst, such as a spent chlorinated catalyst, to less than any maximum chlorine content described herein, for example, less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw of chlorine-containing compounds. Fluoride purging stage

[0115] The methods herein may also include a fluoride purge step. A fluoride purge step may be performed at any point in the methods in this document, such as after a fluorination step. A fluoride purge step may involve contacting a catalyst, such as a decoked and fluorinated catalyst, with a fluoride purge stream. A fluoride purge stream may include any inert gas disclosed in this document, for example, nitrogen.

[0116] A fluoride purge stream may include any of the compounds disclosed in this document, and any of the compounds disclosed in this document may be excluded from a fluoride purge stream. In some embodiments, a fluoride purge stream is substantially free of oxygen-containing compounds. A fluoride purge stream is substantially free of oxygen-containing compounds when oxygen-containing compounds are present in concentrations below Petition 870250083407, dated 09 / 16 / 2025, pp. 244 / 309 43 / 91 approximately 100 ppmw, less than approximately 50 ppmw, or less than approximately 25 ppmw. A fluoride purge stream can be substantially free of halogen-containing compounds (substantially halogen-free). A fluoride purge stream is substantially free of halogen-containing compounds when halogen-containing compounds are present in concentrations less than approximately 100 ppmw, less than approximately 50 ppmw, or less than approximately 25 ppmw.

[0117] A fluoride purging step can be carried out under any effective conditions (e.g., time, temperature, pressure, etc.). In some embodiments, a fluoride purging step is conducted at a fluoride purging temperature in any fluoride purging temperature range disclosed in this document, for example, from about 0°C to about 500°C, from about 0°C to about 400°C, from about 15°C to about 475°C, from about 15°C to about 300°C, or from about 25°C to about 250°C, or from about 25°C to about 450°C, such as about 450°C. A fluoride purge step can be conducted for a period of time within any of the range of fluoride purge time periods disclosed in this document, for example, from about 0.25 hours to about 72 hours, or from about 1 hour to about 48 hours.A fluoride purge step may be conducted for a period of time sufficient to reduce the fluoride content of an outgoing fluoride purge effluent stream, after contact with the decoked and fluorinated catalyst, to less than any maximum fluoride content described herein, for example, less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw of fluoride-containing compounds. Oxygen Purge Stage

[0118] The methods provided in this document may include an oxygen purge step. The oxygen purge step may be performed at any point in the methods provided in this document, such as after a carbon burn-off step or a fluorine purge step.

[0119] An oxygen purge step may include contact with Petition 870250083407, dated 09 / 16 / 2025, pages 245 / 309 44 / 91 a catalyst with an oxygen purge stream. The oxygen purge stream may include any inert gas disclosed in this document, for example, nitrogen. The oxygen purge stream may include any of the compounds disclosed in this document, and any of the compounds disclosed in this document may be excluded from the oxygen purge stream. An oxygen purge stream may be substantially free of oxygen-containing compounds, for example, oxygen-containing compounds may be present in concentrations less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw. The oxygen purge stream may be substantially free of halogen-containing compounds (substantially halogen-free), for example, halogen-containing compounds may be present in concentrations less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw.

[0120] An oxygen purge step can be conducted under any effective conditions (e.g., time, temperature, pressure, etc.). For example, an oxygen purge step can be conducted at an oxygen purge temperature in any of the oxygen purge temperature ranges disclosed in this document, for example, from about 0°C to about 400°C, from about 15°C to about 350°C, from about 25°C to about 325°C, from about 25°C to about 300°C, from about 15°C to about 300°C, from about 25°C to about 260°C, from about 25°C to about 250°C, from about 0°C to about 600°C, from about 15°C to about 550°C, from about 25°C to about 500°C, or from about 25°C to about 450°C. An oxygen purge stage can be conducted for a period of time within any of the oxygen purge time ranges disclosed in this document, for example, from about 0.5 hours to about 96 hours, or from about 1 hour to about 48 hours.An oxygen purge step may be conducted for a period of time sufficient to reduce the oxygen content of the outgoing oxygen purge effluent stream, after contact with the catalyst, to less than any maximum oxygen content described herein, for example. Petition 870250083407, dated 09 / 16 / 2025, pages 246 / 309 45 / 91 less than about 100 ppmw, less than about 50 ppmw, or less than about 25 ppmw of oxygen-containing compounds. Hydrocarbon Treatment Stage

[0121] The methods provided herein may include a hydrocarbon treatment step. A hydrocarbon treatment step may be performed at any point in the methods in this document, such as before a carbon burning step. The hydrocarbon treatment step comprising contact of the spent chlorinated catalyst with a hydrocarbon treatment stream that includes a hydrocarbon feed.

[0122] A hydrocarbon feed may include one or more alkanes and / or one or more cycloalkanes, such as C6-C8 alkanes and / or cycloalkanes.

[0123] A hydrocarbon treatment step can be carried out under any effective conditions (e.g., time, temperature, pressure, etc.). In some embodiments, the hydrocarbon treatment step is conducted at a hydrocarbon treatment temperature in any of the hydrocarbon treatment temperature ranges disclosed in this document, for example, from about 400°C (about 752°F) to about 600°C (about 1,112°F). A hydrocarbon treatment step can be conducted for a period of time in any of the hydrocarbon treatment time ranges disclosed in this document, for example, from about 1 to about 48 hours. Reduction Stage

[0124] The methods provided in this document may include a reduction step. The reduction step may be carried out at any point in the methods provided in this document, such as after the fluorination step. A reduction step may include contacting a catalyst, such as a regenerated catalyst or a coke-free and fluorinated catalyst, with a reducing gas stream. The reducing gas stream may include molecular hydrogen. Petition 870250083407, dated 09 / 16 / 2025, pp. 247 / 309 46 / 91 reducing gas stream may include a molar percentage of molecular hydrogen greater than any minimum amount or within any range disclosed in this document, for example, greater than about 25 molar percent or greater than about 75 molar percent.

[0125] A reduction step can be carried out under any effective conditions (e.g., time, temperature, pressure, etc.). The reduction of a catalyst, such as a regenerated catalyst, can occur at a temperature of about 600°F to about 1200°F, about 700°F to about 1100°F, about 800°F to about 1000°F, about 900°F to about 1000°F, or about 950°F to about 1000°F. The reduction of a catalyst, such as a regenerated catalyst, can occur, at least partially, in an atmosphere that includes an inert gas (such as nitrogen), hydrogen (H2), or a combination thereof. A reduction step can be conducted at a peak reduction temperature in any of the peak reduction temperature ranges disclosed in this document, for example, from about 200°C to about 600°C, or from about 400°C to about 600°C.A reduction step may be initiated at an initial reduction temperature that is the same as any oxygen purge temperature disclosed in this document, for example, in a range of about 0°C to about 600°C, about 15°C to about 550°C, about 25°C to about 500°C, about 25°C to about 450°C, about 0°C to about 500°C, about 0°C to about 300°C, about 20°C to about 250°C, or about 15°C to about 50°C. A reduction step may be conducted for a period of time in any range of reduction step time periods disclosed in this document, for example, from about 0.5 hours to about 48 hours, from about 10 to about 30 hours. Catalysts

[0126] The catalysts subjected to the methods provided herein may include any known catalysts, which may include any known catalyst support. A catalyst support Petition 870250083407, dated 09 / 16 / 2025, pp. 248 / 309 47 / 91 may include a zeolite, an amorphous inorganic oxide, or any combination thereof.

[0127] A catalyst support may include an L-zeolite, a Y-zeolite, a mordenite, an omega zeolite and / or a beta zeolite. A catalyst support may include a potassium L-zeolite or a barium ion-exchanged L-zeolite.

[0128] Catalysts may include a binder, such as a binder that includes alumina, silica, a mixed oxide thereof, or a mixture thereof.

[0129] Catalysts may include a metal, such as a transition metal. The transition metal may include a Group 8-11 transition metal. The transition metal may include platinum. A catalyst may include any range of weight percent of a transition metal; for example, from about 0.1% by weight to about 10% by weight, or from about 0.3% by weight to about 5% by weight, of a transition metal.

[0130] A spent catalyst may include any weight percentage range of a transition metal, such as platinum. For example, a spent catalyst may include a transition metal in any amount from about 0.1% by weight to about 10% by weight, or from about 0.5% by weight to about 2% by weight of platinum.

[0131] In some embodiments, a catalyst includes platinum in a KL zeolite. The catalyst may also include chlorine and fluorine. For example, a catalyst may include any weight percent range of chlorine and / or weight percent range of fluorine disclosed in this document, for example, from about 0.01% by weight to about 5% by weight, or from about 0.3% to about 1.3% by weight of fluorine and / or from about 0.01% by weight to about 5% by weight, from about 0.3% to about 3% by weight, or from about 0.3% to about 1.3% by weight of chlorine. When chlorine and fluorine are present, chlorine and fluorine may be present in any proportion. For example, a catalyst may include a chlorine:fluorine molar ratio of about 0.5:1 to about Petition 870250083407, dated 09 / 16 / 2025, pages 249 / 309 48 / 91 of 4:1. Regenerated / Reactivated Catalysts

[0132] Also provided in this document are catalysts that have been subjected to a method provided in this document, such as reactivated catalysts or regenerated catalysts produced by the method in this document. In some embodiments, the reactivated catalysts or regenerated catalysts include any amount of iron disclosed herein, for example, less than about 400 ppmw, less than about 300 ppmw, less than about 250 ppmw, from about 5 ppmw to about 400 ppmw, from about 50 ppmw to about 300 ppmw, or from about 50 ppmw to about 250 ppmw of iron. In some embodiments, the reactivated catalysts or regenerated catalysts include any amount of iron disclosed herein, for example, the difference in iron concentration between the reactivated catalyst and the spent catalyst is less than about 1.000 ppmw, less than about 600 ppmw, less than about 400 ppmw, from about 5 ppmw to about 600 ppmw, from about 5 ppmw to about 500 ppmw, or from about 5 ppmw to about 300 ppmw of iron.

[0133] In some embodiments, reactivated catalysts or regenerated catalysts include any amount of carbon disclosed herein, for example, less than about 1% by weight, less than about 0.5% by weight, from about 0.01% by weight to about 1% by weight, from about 0.01% by weight to about 0.75% by weight, from about 0.01% by weight to about 0.5% by weight, or from about 0.02% by weight to about 0.5% by weight of carbon.

[0134] In some embodiments, the reactivated catalysts or regenerated catalysts include any amount of chlorine disclosed herein, for example, from about 0.01% by weight to about 5% by weight, from about 0.05% by weight to about 3% by weight, from about 0.05% by weight to about 2.0% by weight, from about 0.3% by weight to about 1.3% by weight of chlorine.

[0135] In some embodiments, the catalysts are reactivated or Petition 870250083407, dated 09 / 16 / 2025, pages 250 / 309 49 / 91 regenerated catalysts include any amount of fluorine disclosed herein, for example, from about 0.01% by weight to about 5% by weight, from about 0.05% by weight to about 3% by weight, from about 0.01% by weight to about 3% by weight, from about 0.1% by weight to about 1.3% by weight, or from about 0.15% by weight to about 1.3% by weight of fluorine.

[0136] In some embodiments, the reactivated catalysts or regenerated catalysts include any amount of fluorine disclosed herein, for example, from about 0.01% by weight to about 5% by weight, from about 0.05% by weight to about 3% by weight, from about 0.01% by weight to about 3% by weight, from about 0.1% by weight to about 1.3% by weight, or from about 0.15% by weight to about 1.3% by weight of fluorine.

[0137] In some embodiments, reactivated or regenerated catalysts are characterized by a TSOR within about 50°F, within about 40°F, within about 30°F, or within about 20°F, of the TSOR of a fresh reference catalyst. A reactivated or regenerated catalyst may be characterized by a TSOR within about 50°F, within about 40°F, within about 30°F, or within about 20°F, of the TSOR of a fresh reference catalyst. A reactivated or regenerated catalyst can be characterized by a fouling rate (FR) in any range disclosed in this document, for example, from about 0.01° F / ha to about 0.25° F / h, from about 0.02° F / ha to about 0.2° F / h, from about 0.03° F / ha to about 0.2° F / h, or from about 0.03° F / ha to about 0.15° F / h.A reactivated or regenerated catalyst can be characterized by a benzene+toluene selectivity in any of the selectivity ranges disclosed in this document, for example, from about 0.88 to about 0.95, or from about 0.89 to about 0.94. A reactivated or regenerated catalyst can be characterized by a benzene+toluene selectivity in any of the selectivity ranges disclosed in this document, for example, greater than 0.88 or greater than 0.90.

[0138] The methods provided here also include methods Petition 870250083407, dated 09 / 16 / 2025, pp. 251 / 309 50 / 91 of the use of a reactivated and / or regenerated catalyst. In some embodiments, the methods include providing a catalyst that has been subjected to any one or more of the regeneration / reactivation methods provided in this document and contacting the catalyst and a reagent, such as a hydrocarbon, to produce a product, such as an aromatic product. EXAMPLES

[0139] The disclosure is further illustrated by the following examples, which should in no way be interpreted as imposing limitations on the scope of this technology. Several other aspects, embodiments, modifications and equivalents thereof may be suggested to one skilled in the art after reading the description in this document, without departing from the spirit of the present disclosure or the scope of the appended claims.

[0140] The weight percentages of Pt, Cl, F, and Fe were determined using X-ray fluorescence (XRF) and are based on the total weight of the aromatization catalyst unless otherwise indicated. Carbon (% by weight) was determined by the CHNS analyzer (Carlo Erba). Platinum dispersions were determined by CO pulse chemisorption.

[0141] The regenerated catalysts in some of the following examples were tested for their respective fouling rates (abbreviated FR, units of °F. / h), which correlate with their activities by the formula, y=FR*t+ TSOR, where y is temperature, FR is the fouling rate, t is time, and TSOR is the initial run-up temperature. The FR of a regenerated catalyst sample was determined by plotting the temperature required to maintain a total aromatic yield of 75% by weight over time under standard test conditions, as described later in this document. The FRs were then determined from the calculated slopes fitted to the resulting data. The total time in the stream was typically 40 hours, and the run-up temperature (abbreviated TEOR) was also determined.

[0142] In each of the examples, the following procedures of Petition 870250083407, dated 09 / 16 / 2025, pp. 252 / 309 51 / 91 standard tests were used. The catalysts were ground and sieved to about 20-40 mesh, and 2 cc of the sieved catalyst were placed in a 1-inch OD stainless steel reactor vessel in a temperature-controlled furnace. After reducing the catalyst under molecular hydrogen flow, a feed stream of aliphatic hydrocarbons (about 12 mL / hour) and molecular hydrogen (about 65 mL / min) was introduced into the reactor vessel, a pressure of about 65 psig, a molar ratio of H2:hydrocarbon of 2.0:1, and a net hourly space velocity (LHSV) of 6 hr-1 to obtain catalyst performance data over time.The aliphatic hydrocarbon feed contained approximately 22 to 32 wt% n-hexane, approximately 4 to 8 wt% n-heptane, approximately 33 to 37 wt% C6 isoparaffins, approximately 15 to 21 wt% C7 isoparaffins, and approximately 6 to 10 wt% C8 isoparaffins, with the balance attributable to C6 and C7 olefins, naphthenes, and aromatics. The reactor effluent composition was analyzed by gas chromatography to determine total aromatics and benzene+toluene selectivity.

[0143] In the examples, experiments were conducted to demonstrate the effectiveness of various processes and steps in regenerating a spent catalyst, with the performance of a fresh flavoring catalyst used as a target baseline. The fresh flavoring catalyst was a Pt / KL-zeolite containing approximately 1 wt% platinum, 0.85 wt% Cl, and 0.70 wt% F, with a BET surface area of ​​approximately 177.5 m² / g, a mercury-intruded pore volume of about 0.19 cc / g, and a micropore volume of about 0.0615 cc / g. The source of the spent catalyst was the fresh catalyst, but after it had been deactivated following long-term use in a flavoring process. Prior to use in these examples, the spent catalyst underwent a mild partial decoking treatment to remove unreacted hydrocarbons and light carbonaceous deposits from the catalyst. EXAMPLE 1A - Preparation of a fluorine-regenerated catalyst Petition 870250083407, dated 09 / 16 / 2025, pp. 253 / 309 52 / 91

[0144] For comparison purposes, the following regeneration procedure, which included the use of fluorine gas, was conducted. Approximately 42 g of spent catalyst were loaded into a new metal fixed-bed reactor (comprising 347 stainless steel), unless otherwise indicated, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 1500 mL / min) for 12 h, then contacted at about 300°F (about 148.9°C) with a nitrogen-containing chlorine gas stream (about 1463 mL / min) and chlorine gas (e.g., a 2% Cl2 in N2 mixture) (about 37 mL / min) for approximately 3 hr, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (1463 mL / min or 1500 mL / min) for approximately 3 hours, or about 12 hours to about 16 hours, then contacted at about 850°F (about 454,4°C) with a decoking gas stream containing a mixture of air (75 mL / min) and nitrogen (1425 mL / min) for approximately 44 hours, then contacted at about 300°F (about 148.9°C) with a gas stream containing nitrogen (about 1350 mL / min) and fluorine gas (e.g., a mixture of F2 in N2) (about 147 mL / min) for approximately 3 hours, and then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 1353 mL / min or about 1500 mL / min) for approximately 3 hours, or about 12 hours to about 16 hours. EXAMPLE 1B - Preparation of a regenerated catalyst with a hydrofluorocarbon in two reactors

[0145] A quantity of spent catalyst was loaded into a new metal fixed-bed reactor (comprising 347 stainless steel), unless otherwise indicated (e.g., in some tests, fluorine gas was in a vessel comprising 347 stainless steel and a hydrofluorocarbon was in a vessel comprising 321 stainless steel). The spent catalyst was then contacted at about 400°F (about 204.4°C) with a stream of nitrogen gas (about 1500 mL / min) for approximately 12 hours, then contacted at about 300°F (about Petition 870250083407, dated 09 / 16 / 2025, pp. 254 / 309 53 / 91 of 148.9°C) with a chlorine gas stream containing nitrogen (about 1463 mL / min) and chlorine gas (e.g., 2% Cl2 in N2) (about 37 mL / min) for approximately 3 hours, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 1463 mL / min) for approximately 3 hours, or about 12 to about 16 hours, then contacted at about 850°F (about 454.4°C) with a decoking gas stream containing air (about 500 mL / min) for approximately 2 hours to produce a coke-free catalyst. The temperature was reduced to 700°F and the airflow was reduced to 200 mL / min. This was repeated several times to make a large batch of chlorinated decoking catalyst.

[0146] Approximately 45 g of the coke-free chloride catalyst were transferred to a reactor (347 stainless steel) with an outside diameter of one inch. A stream of 1,1,1,2-tetrafluoroethane (20%) in N2 at a flow rate of approximately 17 mL / min was combined with a second stream of 200 mL / min of air to produce a combined stream. The coke-free catalyst was contacted with the combined stream at a pressure of 50 psi for approximately 60 minutes. At the end of the 60-minute contact time, the flow of fluorinated organic compound / N2 FREON™ was stopped. A purge continued for 30 minutes with 200 mL / min of air at 730°F and 50 psi. The temperature was reduced to 500°F; once below 500°F, the air was stopped and 200 mL / min of N2 was started. The catalyst was cooled to room temperature in a stream of N2. EXAMPLE 1C - Preparation of a regenerated catalyst with a hydrofluorocarbon in a reactor

[0147] Approximately 60 g of spent catalyst were loaded into a new metal fixed-bed reactor (comprising 321 stainless steel), unless otherwise indicated, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 1700 mL / min) for 12 hours, then contacted at about 300°F (about 148.9°C) with a nitrogen-containing chlorine gas stream (about 1640 mL / min) Petition 870250083407, dated 09 / 16 / 2025, pages 255 / 309 54 / 91 mL / min) and chlorine gas (e.g., a 2% Cl2 in N2 mixture) (about 40 mL / min) for approximately 3 hours, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 1640 mL / min) for approximately 3 hours, or about 12 to about 16 hours, then contacted at about 850°F (about 454.4°C) with an air decoking gas stream (680 mL / min) for approximately 2 hours.

[0148] The airflow was reduced (approximately 280 mL / min) and a stream of 1,1,1,2-tetrafluoroethane (20%) in N2 at a flow rate of approximately 22 mL / min was combined with the air to produce a combined stream. The coke-free catalyst was contacted with the combined stream at a pressure of 50 psi for approximately 60 minutes. At the end of the 60-minute contact time, the flow of fluorinated organic compound / N2 FREON™ was stopped. A purge continued for 30 minutes with 200 mL / min of air at 730°F and 50 psi. The temperature was reduced to 500°F; once below 500°F, the air was stopped and the catalyst was cooled to room temperature in a stream of N2 (approximately 500 mL / min). EXAMPLE 1D - Preparation of a regenerated catalyst with a hydrofluorocarbon in a reactor

[0149] Approximately 30 g of spent catalyst were loaded into a new metal fixed-bed reactor (comprising 321 stainless steel), unless otherwise indicated, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 2363 mL / min) for 12 h, then contacted at about 400°F (about 148.9°C) with a nitrogen-containing chlorine gas stream (about 2333 mL / min) and chlorine gas (e.g., a 2% Cl2 in N2 mixture) (about 30 mL / min) for approximately 3 h, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 2333 mL / min) for approximately 3 hours, or about 12 hours to about 16 hours, It then came into contact at approximately 400°F (approximately 204.4°C) with a stream of decoking gas consisting of air (112 mL / min) and nitrogen (2258 Petition 870250083407, dated 09 / 16 / 2025, pages 256 / 309 55 / 91 mL / min) for approximately 30 min, then it was exposed at approximately 850°F (approximately 454.4°C) to a stream of decoking air (336 mL / min) and nitrogen (2025 mL / min) for approximately 3 hours.

[0150] The air flow continued (approximately 336 mL / min), the nitrogen flow was reduced (approximately 2,000 mL / min), and a stream of 1,1,1,2-tetrafluoroethane (5%) in N2 at a flow rate of approximately 25 mL / min was combined with the air to produce a combined stream. The coke-free catalyst was contacted with the combined stream at a pressure of 50 psi for approximately 60 minutes. At the end of the 60-minute contact time, the flow of fluorinated organic compound / N2 FREON™ was stopped. A purge continued for 30 minutes with the air (approximately 336 mL / min) and nitrogen (approximately 2,000 mL / min) streams at 700°F and 50 psi. The temperature was reduced to 500°F; once below 500°F, the air was stopped and the catalyst was cooled to ambient temperature in the N2 stream.

[0151] The resulting regenerated catalysts were then tested to determine their fluorine concentration. Two samples of the regenerated catalysts were collected from the vertically oriented reactor for testing: a first sample from the upper half of the reactor and a second sample from the lower half of the reactor. The results of these tests are shown in Table 1 below. Table 1 - Results of the regenerated catalysts or results of Example 1D Sample % by weight of F (XRF) Before Regeneration After Regeneration 1A 1B 1C 1D Upper Half of Reactor 0-0.10 1.2 0.56 0.645 0.314 Lower Half of Reactor 0-0.10 0.1 0.38 0.216 0.297 Petition 870250083407, dated 09 / 16 / 2025, pages 257 / 309 56 / 91

[0152] The results in this Table 1 indicated that 1,1,1,2-tetrafluoroethane achieved an improved fluorine distribution in the regenerated catalyst. Although 1,1,1,2-tetrafluoroethane achieved a better distribution in Example 1B than fluorine gas, it should be noted that the previous treatment with 1,1,1,2-tetrafluoroethane was carried out on a spent catalyst that had been treated with the previous chlorine-containing gas stream and a decoking gas stream and then transferred to a different reactor for treatment with 1,1,1,2-tetrafluoroethane. The transfer between reactors may have subjected the catalyst to moisture, which may have improved the fluorine distribution.If this potential exposure to moisture were avoided (for example, by carrying out each of the three steps described above in a single reactor), then the fluorine distribution might not match the previous results, but would, in all probability, still exceed the results achieved with gaseous fluorine by a surprising extent. The same trend in fluorine distribution was also observed in Examples 1C and 1D. The reactivation process in these examples was carried out in a reactor, therefore there was no possibility of exposure to moisture.

[0153] A series of aromatization reactions was then performed to test and compare the adjusted catalyst temperature and the selectivity of the reactivated catalysts: FIG. 2 represents a graph of the adjusted catalyst temperature versus time, and FIG. 3 represents a graph of aromatic selectivity versus time for (1) a fresh aromatization catalyst, (2) a spent aromatization catalyst, (3) a spent aromatization catalyst treated with Cl2 and O2 for 8 hours according to the previous procedure, (4) a spent aromatization catalyst treated with Cl2, O2 and fluorine gas according to Example 1A, and (5) a spent aromatization catalyst subjected to the reactivation procedure of Example 1B, which included treatment of the catalyst with 1,1,1,2-tetrafluoroethane.

[0154] FIG. 4 represents a graph of the adjusted catalyst temperature versus time and FIG. 5 represents a graph of the selectivity of Petition 870250083407, dated 09 / 16 / 2025, pages 258 / 309 57 / 91 aromatics versus time for (1) an embodiment of a fresh flavoring catalyst, (2) an embodiment of a spent flavoring catalyst, and (3) a spent flavoring catalyst subjected to the reactivation procedure of Example 1C, which included treating the catalyst with 1,1,1,2-tetrafluoroethane.

[0155] FIG. 6 represents a graph of the adjusted catalyst temperature versus time, and FIG. 7 represents a graph of aromatic selectivity versus time for (1) an embodiment of a fresh flavoring catalyst, (2) an embodiment of a spent flavoring catalyst, and (3) a spent flavoring catalyst subjected to the reactivation procedure of Example 1D, which included treatment of the catalyst with 1,1,1,2-tetrafluoroethane.

[0156] The data in FIG.2—FIG. 7 demonstrated that an activity substantially equivalent to the activity of the fresh catalyst could be restored using fluorine gas or the fluorinated organic compound FREON™ as the fluorine source. EXAMPLE 2 - Preparation of a regenerated catalyst with a hydrofluorocarbon using a downstream reactor

[0157] The fluorinated organic compound FREON™ can be used as a fluorinating agent. When the fluorinated organic compound FREON™ is used, a temperature at which a spent catalyst is brought into contact with the fluorinated organic compound FREON™ can be between 700°F and 850°F in order to decompose the fluorinated organic compound FREON™, thus allowing fluorine to deposit on the spent catalyst.

[0158] Laboratory-scale tests included one-pass fluoridation over a spent catalyst with FREON™ fluorinated organic compound in nitrogen, with up to 3% oxygen. When one pass was used, it was observed that a temperature of at least 850°F was required to decompose a desired portion of the FREON™ fluorinated organic compound to deposit fluorine on the catalyst. Petition 870250083407, dated 09 / 16 / 2025, pages 259 / 309 58 / 91

[0159] The distribution of fluorine through the catalyst bed, however, was generally poor in these laboratory-scale tests, and there were concerns regarding the furnace / reactor metallurgy.

[0160] Therefore, lower decomposition temperatures were tested. At the lower decomposition temperatures, one pass resulted in the decomposition of only a small portion of the fluorinated organic compound FREON™, but the distribution of fluorine across the catalyst bed was improved. Lower temperatures, therefore, were advantageous in some respects.

[0161] If this procedure were carried out in commercial units where all furnaces / reactors were maintained at decomposition temperatures, only a portion of the fluorinated organic compound FREON™ would decompose, and then contact with each subsequent catalyst bed would deposit a similar portion of Freon into the feed (now lower than the previous bed), which was believed to cause uneven loading and possibly other problems. There were also concerns that the decomposition of the fluorinated organic compound FREON™ in a furnace could produce hydrogen fluoride and potentially damage the furnace metal or other component of a system. Therefore, maintaining the target reactor at an appropriate temperature to decompose the Freon while keeping the rest of the plant below the decomposition temperature of the fluorinated organic compound FREON™ and recycling the reactor effluent back to the target reactor would ensure proper fluorine loading into the catalyst.To show that Freon or decomposition products in the effluent from the target reactor would not affect downstream metallurgy, the following test was performed; the results of one of these tests are provided in Table 2 below. In the test, a stream containing fluorine (which included the fluorinated organic compound FREON™) was sequentially circulated through Reactor 1, a furnace tube, and Reactor 2. Reactor 1 and Reactor 2 contained spent catalyst that had been previously dried, chlorided, purged, and oxidized as described in Example 1D. The furnace tube was filled with... Petition 870250083407, dated 09 / 16 / 2025, pages 260 / 309 59 / 91 support spheres, which were added to aid in heat transfer. Table 2 - Results of Example 2 (Single Passage) Reactor 1 Result / Configuration: Furnace Tube, Reactor 2 Temperature: 730°F, 700°F, 600°F. % by weight of FREON™ fluorinated organic compound that decomposed: 20% by weight - -. % by weight of fluorine present in the catalyst: 0.295% by weight - 0.06% by weight.

[0162] To alleviate one or more of these concerns, fluorination was carried out by maintaining only one furnace / reactor at a decomposition temperature, i.e., a fluorination temperature. By maintaining the temperature of the other furnaces / reactors below the decomposition temperature, the decomposition of the fluorinated organic compound FREON™ was reduced or minimized in the furnaces / reactors at the lower temperatures and, as a result, a significant portion of the fluorinated organic compound FREON™, if any, would not be deposited in these reactors. EXAMPLE 3 - Preparation of a regenerated catalyst with a recycled hydrofluorocarbon

[0163] Approximately 61 g of spent catalyst were loaded into a metal fixed-bed reactor (comprising 321 stainless steel), unless otherwise indicated, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 9291 mL / min) for about 12 h, then contacted at about 400°F (about 148.9°C) with a nitrogen-containing chlorine gas stream (about 9236 mL / min) and chlorine gas (e.g., a 2% Cl2 in N2 mixture) (about 55 mL / min) for about 3 h, then contacted at about 400°F (about 204.4°C) with a nitrogen gas stream (about 9236 mL / min) Petition 870250083407, dated 09 / 16 / 2025, pp. 261 / 309 60 / 91 mL / min) for approximately 3 hours, or about 12 hours to about 16 hours, then came into contact at about 400°F (about 204.4°C) with a stream of air (444 mL / min) and nitrogen (8847 mL / min) decoking gas for approximately 30 min, then came into contact at about 850°F (about 454.4°C) with a stream of air (1325 mL / min) and nitrogen (7966 mL / min) decoking gas for approximately 3 hours.

[0164] The air flow (approximately 258 mL / min) and the nitrogen flow (approximately 1522 mL / min) were fed to the reactor. While the air and nitrogen mixture was flowing into the reactor, the compressor was set to deliver 1800 sccm of total flow back to the reactor. The recycle flow was verified using a flow measurement system installed in the recycle circuit (or, in other words, feedback circuit, such as feedback circuit 102 shown in FIG. 1). Once the recycle flow rate was confirmed, the air and nitrogen feed mixture was stopped while simultaneously locking the reactor system with the recycle circuit. This allowed the system to operate in 100% recycle mode without flowing fresh gas into the reactor and maintaining the reactor pressure at 50 psig.The recycling cycle was run for 10 minutes, then a stream of 1,1,1,2-tetrafluoroethane (5%) in N2 at a flow rate of 20 mL / min was combined with the recycling stream at the reactor inlet to produce a combined stream. The coke-free catalyst was contacted with the combined stream at 730°F and 50 psig pressure. After 10 minutes, a gas bag sample was collected from the reactor effluent, as shown in FIG. 1. At 60 minutes, the flow of fluorinated organic compound FREON™ was stopped and the compressor continued to run in the recycling circuit for 120 minutes. A second sample bag was taken at 180 minutes. The compressor was stopped and the reactor was purged with a combined air (approximately 286 mL / min) and nitrogen streams (approximately 1714 mL / min) at 730°F and 50 psi for 30 minutes. The reactor was cooled to ambient temperature using a flow of air and nitrogen. Petition 870250083407, dated 09 / 16 / 2025, pp. 262 / 309 61 / 91 Table 3 - Results of Example 3 Sample Time after the start of Freon introduction into the reactor (min) % of Freon from the initial concentration Feed — 100 Gas bag 1 10 51 Gas bag 2 180 1.1

[0165] During reactivation, the fluorinated organic compound FREON™ was then transported around a recycling loop back to the target furnace / reactor, i.e., the furnace / reactor maintained at a decomposition temperature. This procedure sometimes requires multiple passes of the fluorinated organic compound FREON™ through the recycling loop, but it is believed that this procedure maximizes the amount of fluorine that comes into contact with and is placed in the target reactor, i.e., the reactor maintained at a decomposition temperature. ASPECTS

[0166] The following is a list of non-limiting aspects:

[0167] Aspect 1. Reform method, characterized in that it comprises, consists essentially of, or consists of any two or more of the following steps:

[0168] (A) contacting a hydrocarbon feed with an aromatization catalyst comprising a transition metal and a catalyst carrier under reforming conditions in a metal reactor system to produce an aromatic product;

[0169] (B) carry out step (A) for a period of time sufficient to form a spent catalyst;

[0170] (C) contact the spent catalyst with hydrogen gas to produce a spent catalyst removed;

[0171] (D) subject the removed spent catalyst to a burn of Petition 870250083407, dated 09 / 16 / 2025, pp. 263 / 309 62 / 91 carbon at a temperature, such as a temperature not exceeding about 500°F, for a time effective to remove from the spent catalyst at least a portion of the hydrogen carbon feed, at least a portion of the aromatic product, or a combination thereof, to form a treated spent catalyst;

[0172] (E) contacting the treated spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst;

[0173] (F) subjecting the spent chlorinated catalyst to a carbon burn at a temperature, such as a temperature not exceeding 900°F, for a time effective to improve a dispersion of the transition metal in the spent chlorinated catalyst to form a redistributed spent catalyst; and

[0174] (G) contacting the spent redistributed catalyst with a fluorine-containing stream comprising a fluorine-containing compound to form a regenerated catalyst; and

[0175] (H) reduce the regenerated catalyst.

[0176] Aspect 2. The method defined in aspect 1, where the reforming method is an in situ process, for example, steps (A)-(H) are carried out in the same reactor system.

[0177] Aspect 3. The method defined in aspect 1, wherein the (C)-(H) steps are carried out externally to the reactor system of the (A)(B) steps, for example, the (C)-(H) steps are carried out in a metal reactor that is not in the reforming reactor system.

[0178] Aspect 4. The method defined in any of aspects 1-3, further comprising a catalyst reactivation step after step (H).

[0179] Aspect 5. Method for regenerating a spent catalyst, characterized in that it comprises a transition metal and a catalyst support in a metal reactor, the method comprising, consisting essentially of, or comprising any two or more of the following Petition 870250083407, dated 09 / 16 / 2025, pp. 264 / 309 63 / 91 steps:

[0180] (1) contact the spent catalyst with hydrogen gas to produce a spent catalyst removed;

[0181] (2) subjecting the removed spent catalyst to a carbon burn at a temperature, such as a temperature not exceeding about 500°F, for a time effective to remove from the spent catalyst at least a portion of the hydrogen carbon feed, at least a portion of the aromatic product, or a combination thereof to form a treated spent catalyst;

[0182] (3) contacting the treated spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst;

[0183] (4) subjecting the spent chlorinated catalyst to a carbon burn at a temperature, such as a temperature not exceeding 900°F, for a time effective to improve a dispersion of the transition metal in the spent chlorinated catalyst to form a redistributed spent catalyst;

[0184] (5) contacting the spent redistributed catalyst with a fluorine-containing stream comprising a fluorine-containing compound to form a regenerated catalyst; and

[0185] (6) reduce the regenerated catalyst.

[0186] Aspect 6. Reform method, characterized in that it comprises, consists essentially of, or consists of any two or more of the following steps:

[0187] (A) contacting a hydrocarbon feed with an aromatization catalyst comprising a transition metal and a catalyst carrier under reforming conditions in a metal reactor system to produce an aromatic product;

[0188] (B) perform step (A) for a period of time sufficient to form a spent catalyst;

[0189] (C) contact the spent catalyst with a stream containing Petition 870250083407, dated 09 / 16 / 2025, pages 265 / 309 64 / 91 chlorine comprising a chlorine-containing compound for producing a chlorinated spent catalyst, wherein, optionally, the chlorine-containing compound comprises chlorine, a chlorinated hydrocarbon, a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC) or a combination thereof;

[0190] (D) contacting the spent chlorinated catalyst with a decoking gas stream comprising oxygen to produce a decoked catalyst; and

[0191] (E) contacting the coke-free catalyst with a fluorine-containing stream comprising a fluorine-containing compound, wherein the fluorine-containing compound comprises a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC), a fluorocarbon (FC) or a combination thereof.

[0192] Aspect 7. The method defined in aspect 6, where the reforming method is an in situ process, for example, steps (A)-(E) are carried out in the same reactor system.

[0193] Aspect 8. The method defined in aspect 6, wherein steps (C)-(E) are performed externally to the reactor system of steps (A)(B), for example, steps (C)-(E) are performed in a metal reactor that is not in the reforming reactor system.

[0194] Aspect 9. The method defined in any of aspects 6-8, further comprising a catalyst reactivation step after step (E).

[0195] Aspect 10. Method for regenerating a spent catalyst, characterized in that it comprises a transition metal and a catalyst support in a metal reactor, the method comprising, consisting essentially of, or consisting of:

[0196] (1) contacting the spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst;

[0197] (2) contact the spent chlorinated catalyst with a stream Petition 870250083407, dated 09 / 16 / 2025, pages 266 / 309 65 / 91 decoking gas comprising oxygen to produce a decoked catalyst; and

[0198] (3) contacting the coke-free catalyst with a fluorine-containing stream comprising a fluorine-containing compound to produce a regenerated catalyst, wherein the fluorine-containing compound comprises a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC), a fluorocarbon (FC) or a combination thereof.

[0199] Aspect 11. The method defined in any of the preceding aspects, wherein the contact of the spent catalyst with hydrogen gas occurs, at least in part, at a temperature above 25°F, above 100°F, above 200°F, above 300°F, above 400°F or above 500°F.

[0200] Aspect 12. The method defined in any of the preceding aspects, wherein the contact of the spent catalyst with hydrogen gas occurs, at least in part, at a temperature of about 300°F to about 800°F, about 400°F to about 800°F, or about 500°F to about 800°F.

[0201] Aspect 13. The method defined in any of the preceding aspects, wherein the contact of the spent catalyst with hydrogen gas occurs for a time of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours or about 1 minute to about 2 hours.

[0202] Aspect 14. The method defined in any of the preceding aspects, in which the fluorine-containing compound comprises, consists essentially of, or is made up of, a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC), a fluorocarbon (FC), or a combination thereof.

[0203] Aspect 15. The method defined in any of the preceding aspects, wherein the fluorine-containing stream comprises (or essentially consists of, or consists of) (i) the fluorine-containing compound and any inert gas disclosed in this document, for example, nitrogen, (ii) the compound Petition 870250083407, dated 09 / 16 / 2025, pp. 267 / 309 66 / 91 containing fluorine, any inert gas disclosed in this document and air, (iii) the compound containing fluorine and air, or (iv) the compound containing fluorine, oxygen (O2) and any inert gas disclosed in this document, for example, nitrogen; wherein when the fluorine-containing stream includes an inert gas and air, the inert gas and air may be present in a volume ratio of about 3:1 to about 30:1, about 3:1 to about 20:1, about 3:1 to about 10:1, about 3:1 to about 5:1 or about 4:1; or the volume ratio of inert gas to oxygen (O2) in the fluorine-containing stream is about 90:10 to about 99.9:0.1, about 95:5 to about 99:1 or about 97:3 (inert gas: oxygen (O2)).

[0204] Aspect 16. The method defined in any of the preceding aspects, in which the contact of the redistributed spent catalyst with a fluorine-containing stream comprises (essentially consists of, or consists of) circulating the inert gas and injecting the fluorine-containing compound into the circulating inert gas.

[0205] Aspect 17. The method defined in any of the preceding aspects, wherein the injection of the fluorine-containing compound is achieved, at least in part, with a spray apparatus configured to disperse the fluorine-containing compound in the circulating inert gas.

[0206] Aspect 18. The method defined in any of the preceding aspects, wherein the contact of the spent redistributed catalyst with a fluorine-containing stream comprises (essentially consists of, or consists of) circulating a stream comprising the inert gas and oxygen (O2) and injecting the fluorine-containing compound into the circulating stream.

[0207] Aspect 19. The method defined in any of the preceding aspects, wherein oxygen (O2) is present in the circulating stream at a concentration of about 0.01% to about 10%, about 0.01% to about 8%, about 0.01% to about 6%, about 0.01% to about 4%, about 1% to about 4%, about 2% to about 4%, about 2.5% to about 3.5%, or about 3%, by volume.

[0208] Aspect 20. The method defined in any of the Petition 870250083407, dated 09 / 16 / 2025, pp. 268 / 309 67 / 91 previous aspects, wherein (i) an amount of fluorine-containing compound in the fluorine-containing stream, (ii) a duration of contact of the spent catalyst with the fluorine-containing stream, or (iii) a combination thereof is selected to place in the spent catalyst redistributed about 0.1% by weight to about 2% by weight, about 0.5% by weight to about 1.5% by weight, about 0.5% by weight to about 1% by weight, or about 0.8% by weight to about 1% by weight of fluorine.

[0209] Aspect 21. The method defined in any of the preceding aspects, wherein the contact of the spent catalyst and the fluorine-containing stream occurs, at least partially, at a temperature of about 500°F to about 1,000°F, about 600°F to about 1,000°F, about 600°F to about 900°F, about 700°F to about 900°F, or about 700°F to about 850°F.

[0210] Aspect 22. The method defined in any of the above aspects, wherein the fluorine-containing compound comprises (or consists essentially of, or consists of):

[0211] (i) a compound of formula (I)

[0212] CaHbClcFd Formula (I),

[0213] where

[0214] a is from 1 to 6,

[0215] b is 0 to 14,

[0216] c is 0 to 14,

[0217] d is 1 to 14,

[0218] where, optionally, be / or c is not 0, and

[0219] where b + c + d = 2a + 2,

[0220] in which, optionally, the compound of formula (I) is replaced;

[0221] (ii) 1,1,1,2-tetrafluoroethane;

[0222] (iii) difluoromethane; or

[0223] (iv) dichlorodifluoromethane. Petition 870250083407, dated 09 / 16 / 2025, pp. 269 / 309 68 / 91

[0224] Aspect 23. The method defined in any of the above aspects, wherein the fluorine-containing compound consists of 1,1,1,2-tetrafluoroethane.

[0225] Aspect 24. The method defined in any of the preceding aspects, wherein the amount of fluorine-containing compound in the fluorine-containing stream is controlled to give a fluorine [F] concentration in the catalyst less than any maximum amount or within any range disclosed in this document, for example, less than about 10% by weight, less than about 8% by weight, less than about 6% by weight, less than about 4% by weight, less than about 2% by weight, less than 1.5% by weight, within a range of about 0.1% by weight to about 3% by weight, about 1% by weight to about 2% by weight, about 1.25% by weight to about 1.75% by weight, about 0.1% by weight to about 1.0% by weight, about 0.5% by weight to about 1% by weight, or about 0.3% by weight to about 0.8% by weight.

[0226] Aspect 25. The method defined in any of the preceding aspects, wherein the fluorine-containing stream is substantially free of oxygen-containing compounds and / or chlorine-containing compounds that do not include a fluorine atom, for example, less than about 100 ppmw, less than about 50 ppmw or less than about 25 ppmw.

[0227] Aspect 26. The method defined in any of the preceding aspects, wherein the amount of fluorine-containing compound in the fluorine-containing stream is controlled to give a concentration of fluorine (F) or fluorine-containing compound less than any maximum amount or in any range disclosed in this document, for example, less than about 50,000 ppmv, in a range of about 5 to about 25,000 ppmv, in a range of about 10 to about 25,000 ppmv, in a range of about 50 to about 25,000 ppmv, in a range of about 5,000 to about 25,000 ppmv, in a range of about 50 to about 20,000 ppmv, in a range of about 50 to about 15,000 ppmv, in a range of about 50 to about 10,000 ppmv, in a range Petition 870250083407, dated 09 / 16 / 2025, pp. 270 / 309 69 / 91 from about 50 to about 5,000 ppmv, in a range of about 50 to about 2,500 ppmv, in a range of about 50 to about 1,000 ppmv, in a range of about 500 to about 1,000 ppmv, in a range of about 600 to about 900 ppmv, in a range of about 700 to about 800 ppmv, or about 750 ppmv.

[0228] Aspect 27. The method defined in any of the preceding aspects, wherein the fluorination step is conducted at (i) a fluorination temperature in any fluorination temperature range disclosed in this document, for example, from about 0°C to about 600°C, from about 10°C to about 550°C, from about 20°C to about 450°C, from about 0°C to about 300°C, from about 20°C to about 250°C, or from about 15°C to about 50°C, (ii) a fluorination pressure of atmospheric pressure to about 15 bar, atmospheric pressure to about 10 bar, atmospheric pressure to about 7 bar, from about 0.5 bar to about 10 bar, from about 0.5 bar to about 5 bar, from about 0.5 bar to about 1.5 bar, about 1 bar, about 2 bar to about 10 bar, about 2 bar to about 5 bar or about 2 bar.

[0229] Aspect 28. The method defined in any of the preceding aspects, wherein the fluorination step is carried out for a period of time in any range of fluorination time periods disclosed in this document, for example, from about 0.5 hours to about 96 hours, from about 0.5 hours to about 72 hours, from about 0.5 to about 48 hours, from about 0.5 to about 12 hours, from about 0.5 to about 8 hours, from about 0.1 hour to about 96 hours, from about 0.1 hour to about 72 hours, from about 0.1 to about 48 hours, from about 0.1 to about 12 hours, or from about 0.1 to about 8 hours.

[0230] Aspect 29. The method defined in any of the preceding aspects, wherein the chlorine-containing stream comprises (or essentially consists of, or consists of) the chlorine-containing compound and any inert gas disclosed in this document, for example, nitrogen.

[0231] Aspect 30. The method defined in any of the preceding aspects, further comprising the circulation of the inert gas and the injection. Petition 870250083407, dated 09 / 16 / 2025, pp. 271 / 309 70 / 91 of the chlorine-containing compound in the circulating inert gas.

[0232] Aspect 31. The method defined in any of the preceding aspects, wherein the injection of the chlorine-containing compound is achieved, at least in part, by means of a spray apparatus configured to disperse the chlorine-containing compound in the circulating inert gas.

[0233] Aspect 32. The method defined in any of the preceding aspects, wherein the chlorine-containing stream comprises (or consists essentially of, or consists of) chlorine gas (Cl2) and nitrogen.

[0234] Aspect 33. The method defined in any of the preceding aspects, wherein the amount of chlorine-containing compound in the chlorine-containing stream is controlled to give a concentration of chlorine (Cl) or chlorine-containing compound less than any maximum amount or in any range disclosed in this document, for example, less than about 50,000 ppmv, in a range of about 5 to about 25,000 ppmv, in a range of about 10 to about 25,000 ppmv, in a range of about 50 to about 25,000 ppmv, in a range of about 50 to about 20,000 ppmv, in a range of about 50 to about 15,000 ppmv, in a range of about 50 to about 10,000 ppmv, in a range of about 50 to about 5,000 ppmv, in a range of about 50 to about 2,500 ppmv, in a range of about 50 to about 1.000 ppmv, in a range of about 50 to about 500 ppmv, in a range of about 50 to about 100 ppmv, in a range of about 100 to about 750 ppmv, or in a range of about 500 to about 600 ppmv.

[0235] Aspect 34. The method defined in any of the preceding aspects, wherein (i) the amount of chlorine or chlorine-containing compound in the chlorine-containing stream, (ii) the duration of contact of the treated spent catalyst and the chlorine-containing stream, or (iii) a combination thereof is controlled to place in the treated spent catalyst about 0.1% by weight to about 2% by weight, about 0.5% by weight to about 1.5% by weight, about 0.5% by weight to about 1% by weight, or 0.6% by weight to about 1% by weight of chlorine or the chlorine-containing compound. Petition 870250083407, dated 09 / 16 / 2025, pp. 272 / 309 71 / 91

[0236] Aspect 35. The method defined in any of the preceding aspects, wherein the chlorine-containing stream is substantially free of oxygen-containing compounds and / or fluorine-containing compounds, for example, less than about 100 ppmw.

[0237] Aspect 36. The method defined in any of the preceding aspects, wherein the chlorination step is conducted at a chlorination temperature in any chlorination temperature range disclosed in this document, for example, from about 0°F to about 600°F, from about 100°F to about 600°F, from about 200°F to about 600°F, from about 3000°F to about 600°F, from about 400°F to about 600°F, from about 400°F to about 500°F, from about 400°F to about 450°F, from about 300°F to about 500°F, from about 350°F to about 500°F, or from about 350°F to about 450°F.

[0238] Aspect 37. The method defined in any of the preceding aspects, wherein the chlorination step is carried out for a period of time in any range of chlorination time periods disclosed in this document, for example, from about 0.5 hours to about 72 hours, from about 0.75 hours to about 60 hours, from about 1 to about 48 hours, from about 1 to about 12 hours, from about 2 to about 8 hours, from about 0.10 hours to about 72 hours, from about 0.50 hours to about 60 hours, from about 0.5 to about 48 hours, from about 0.5 to about 12 hours, or from about 1 to about 8 hours.

[0239] Aspect 38. The method defined in any of the preceding aspects, wherein the decoking gas stream comprises (or essentially consists of, or consists of) any combination of an inert gas (one or more) and oxygen disclosed in this document, for example, a mixture of nitrogen and oxygen, air or a mixture of air and nitrogen.

[0240] Aspect 39. The method defined in any of the preceding aspects, wherein the decoking gas stream comprises a molar % of oxygen less than any maximum amount or in Petition 870250083407, dated 09 / 16 / 2025, pp. 273 / 309 72 / 91 any range disclosed in this document, for example, less than about 5% molar, in a range of about 0.1 to about 10% molar, in a range of about 0.1 to about 8% molar, in a range of about 0.1 to about 5% molar, in a range of about 0.5 to about 3% molar, or in a range of about 0.5 to about 6% molar.

[0241] Aspect 40. The method defined in any of the preceding aspects, wherein the decoking gas stream is substantially free of halogen-containing compounds, such as added halogen-containing compounds (e.g., substantially halogen-free, substantially chlorine-free), for example, less than about 100 ppmw.

[0242] Aspect 41. The method defined in any of the above aspects, wherein the decoking gas stream is substantially free of water (e.g., added water), for example, less than about 100 ppmw.

[0243] Aspect 42. The method defined in any of the above aspects, wherein the carbon burning temperature of the removed spent catalyst is from about 300°F to about 600°F, from about 350°F to about 550°F, from about 350°F to about 500°F, from about 400°F to about 475°F.

[0244] Aspect 43. The method defined in any of the preceding aspects, wherein the burning of carbon from the removed spent catalyst occurs for a time of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours, or about 1 minute to about 2 hours.

[0245] Aspect 44. The method defined in any of the preceding aspects, wherein the carbon burn-off of the removed spent catalyst removes at least 90% by weight, at least 95% by weight, at least 99% by weight or 100% by weight of the hydrocarbon feed from the spent catalyst.

[0246] Aspect 45. The method defined in any of the Petition 870250083407, dated 09 / 16 / 2025, pages 274 / 309 73 / 91 previous aspects, whereby the carbon burn from the removed spent catalyst removes at least 90% by weight, at least 95% by weight, at least 99% by weight or 100% by weight of the aromatic product from the spent catalyst.

[0247] Aspect 46. The method defined in any of the preceding aspects, wherein a quantity of soft coke is absorbed and / or adsorbed onto the spent catalyst and the burning of carbon from the removed spent catalyst reduces the quantity of soft coke absorbed and / or adsorbed onto the spent catalyst.

[0248] Aspect 47. The method defined in any of the above aspects, wherein the carbon combustion temperature of the spent chlorinated catalyst is about 500°F to about 1,200°F, about 500°F to about 1,100°F, about 500°F to about 1,000°F, about 600°F to about 1,000°F, about 700°F to about 1,000°F, about 700°F to about 900°F, about 800°F to about 900°F or about 850°F.

[0249] Aspect 48. The method defined in any of the above aspects, wherein the carbon burning of the spent chlorinated catalyst occurs for a time of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours or about 1 minute to about 2 hours.

[0250] Aspect 49. The method defined in any of the above aspects, wherein the carbon burning of the chlorinated catalyst improves the dispersion of the transition metal in the spent chlorinated catalyst by at least 40%, at least 50%, at least 60%, at least 70%, at least 80% or at least 90%.

[0251] Aspect 50. The method defined in any of the above aspects, wherein the carbon combustion temperature of the spent chlorinated catalyst is about 500°F to about 1,200°F, about 500°F to about 1,100°F, about 500°F to about 1,000°F, about 600°F to about 1,000°F, about 700°F to about 1,000°F, about 700°F to about 900°F, about 800°F to about 900°F or about 850°F. Petition 870250083407, dated 09 / 16 / 2025, pp. 275 / 309 74 / 91

[0252] Aspect 51. The method defined in any of the aspects above, wherein the carbon burning of the spent chlorinated catalyst occurs for a time of about 1 minute to about 24 hours, about 1 minute to about 18 hours, about 1 minute to about 12 hours, about 1 minute to about 6 hours or about 1 minute to about 2 hours.

[0253] Aspect 52. The method defined in any of the preceding aspects, wherein the carbon burning of the chlorinated catalyst improves the dispersion of the transition metal in the spent chlorinated catalyst by at least 40%, at least 50%, at least 60%, at least 70%, at least 80% or at least 90%.

[0254] Aspect 53. The method defined in any of the preceding aspects, wherein a carbon burning step is conducted at a peak decoking temperature in any of the peak decoking temperature ranges disclosed in this document, for example, from about 100°C to about 700°C, from about 125°C to about 650°C, from about 150°C to about 600°C, from about 200°C to about 500°C, or from about 350°C to about 450°C.

[0255] Aspect 54. The method defined in any of the preceding aspects, wherein a carbon burning step is initiated at an initial decoking temperature which is the same as any chlorine purge temperature disclosed in this document, for example, from about 0°C to about 300°C, from about 20°C to about 275°C, from about 20°C to about 250°C, or from about 50°C to about 200°C.

[0256] Aspect 55. The method defined in any of the preceding aspects, wherein the carbon burning step is conducted for a period of time in any range of decoking time periods disclosed in this document, for example, from about 0.5 hours to about 120 hours, from about 0.75 hours to about 108 hours, from about 1 hour to about 96 hours, from about 1 hour to about 72 hours, from about 12 hours to about 48 hours or from about 1 hour to about 6 hours. Petition 870250083407, dated 09 / 16 / 2025, pp. 276 / 309 75 / 91

[0257] Aspect 56. The method defined in any of the preceding aspects, wherein the carbon burning step is carried out for a period of time sufficient to reduce the % by weight of carbon in the spent chlorinated catalyst to less than any maximum % by weight of carbon disclosed in this document, for example, less than about 1% by weight, less than about 0.5% by weight or less than about 0.2% by weight.

[0258] Aspect 57. The method defined in any of the preceding aspects, wherein the method further comprises a partial decoction step before the chlorination step, the partial decoction step comprising contacting the spent catalyst with a partial decoction gas stream comprising oxygen.

[0259] Aspect 58. The method defined in any of the preceding aspects, wherein the partial decoking gas stream comprises (or essentially consists of, or consists of) any combination of an inert gas (one or more) and oxygen disclosed in this document, for example, a mixture of nitrogen and oxygen, or air.

[0260] Aspect 59. The method defined in any of the preceding aspects, wherein the partial decoking gas stream comprises a molar % of oxygen less than any maximum amount or in any range disclosed in this document, for example, less than about 5 molar %, or in a range of about 0.5 to about 3 molar %, about 1 to about 3 molar %, about 0.1 to about 4 molar %, or about 0.1 to about 3 molar %.

[0261] Aspect 60. The method defined in any of the preceding aspects, wherein the partial decoking gas stream is substantially free of halogen-containing compounds (e.g., substantially halogen-free), for example, less than about 100 ppmw.

[0262] Aspect 61. The method defined in any of the Petition 870250083407, dated 09 / 16 / 2025, pp. 277 / 309 76 / 91 previous aspects, where the decoking gas stream is substantially free of water, for example, less than about 100 ppmw.

[0263] Aspect 62. The method defined in any of the preceding aspects, wherein the partial decoction step is carried out at a partial decoction temperature in any partial decoction temperature range disclosed in this document, for example, from about 150°C to about 600°C, from about 150°C to about 250°C.

[0264] Aspect 63. The method defined in any of the preceding aspects, wherein the partial decoking step is conducted for a period of time in any range of partial decoking time periods disclosed in this document, for example, from about 1 hour to about 48 hours, or from about 2 to about 24 hours.

[0265] Aspect 64. The method defined in any of the preceding aspects, wherein the partial decoking step is carried out for a period of time sufficient to reduce the % by weight of carbon in the spent catalyst to any range of % by weight of carbon disclosed in this document, for example, from about 0.05% by weight to about 10% by weight, from about 0.1% by weight to about 10% by weight, from about 0.05% by weight to about 5% by weight, from about 0.1% by weight to about 5% by weight, from about 1% by weight to 10% by weight, or from about 4% by weight to about 5% by weight.

[0266] Aspect 65. The method defined in any of the preceding aspects, wherein the method further comprises a pre-drying step before the chlorination step, the pre-drying step comprising contacting the spent catalyst with a pre-drying gas stream comprising (or consisting essentially of, or consisting of) any inert gas disclosed in this document, for example, nitrogen.

[0267] Aspect 66. The method defined in any of the preceding aspects, wherein the pre-drying gas stream is substantially free of oxygen-containing compounds, for example, less than Petition 870250083407, dated 09 / 16 / 2025, pages 278 / 309 77 / 91 approximately 100 ppmw.

[0268] Aspect 67. The method defined in any of the preceding aspects, wherein the pre-drying step is carried out at a pre-drying temperature in any of the pre-drying temperature ranges disclosed in this document, for example, from about 75°C to about 500°C, from about 100°C to about 500°C, from about 0°C to about 400°C, from about 100°C to about 400°C, from about 125°C to about 300°C, or from about 180°C to about 280°C.

[0269] Aspect 68. The method defined in any of the preceding aspects, wherein the pre-drying step is carried out for a period of time in any range of pre-drying time periods disclosed in this document, for example, from about 1 hour to about 96 hours, or from about 1 hour to about 48 hours.

[0270] Aspect 69. The method defined in any of the preceding aspects, wherein the pre-drying step is carried out for a period of time sufficient to reduce the moisture content of the spent catalyst to less than any maximum spent catalyst moisture content disclosed in this document, for example, less than about 4% by weight, or less than about 1% by weight.

[0271] Aspect 70. The method defined in any of the preceding aspects, wherein the method further comprises a chlorine purge step before the carbon burning step, the chlorine purge step comprising contacting the spent chlorinated catalyst with a chlorine purge stream comprising (or consisting essentially of, or consisting of) any inert gas disclosed in this document, for example, nitrogen.

[0272] Aspect 71. The method defined in any of the preceding aspects, wherein the chlorine purge stream is substantially free of oxygen-containing compounds, for example, less than about 100 ppmw. Petition 870250083407, dated 09 / 16 / 2025, pp. 279 / 309 78 / 91

[0273] Aspect 72. The method defined in any of the preceding aspects, wherein the chlorine purge stream is substantially free of halogen-containing compounds (substantially halogen-free), for example, less than about 100 ppmw.

[0274] Aspect 73. The method defined in any of the preceding aspects, wherein the chlorine purge step is conducted at a chlorine purge temperature in any chlorine purge temperature range disclosed in this document, for example, from about 0°C to about 400°C, from about 15°C to about 350°C, from about 15°C to about 300°C, or from about 25°C to about 250°C.

[0275] Aspect 74. The method defined in any of the preceding aspects, wherein the chlorine purge step is conducted for a period of time in any range of chlorine purge time periods disclosed in this document, for example, from about 1 hour to about 96 hours, from about 1 hour to about 48 hours.

[0276] Aspect 75. The method defined in any of the preceding aspects, wherein the chlorine purge step is carried out for a period of time sufficient to reduce the chlorine content of the outgoing chlorine purge effluent stream, after contact with the spent chlorinated catalyst, to less than any maximum chlorine content described herein, for example, less than about 100 ppmw of chlorine-containing compounds.

[0277] Aspect 76. The method defined in any of the preceding aspects, wherein the method further comprises a fluorine purge step after the fluorination step, the fluorine purge step comprising contacting the decoked and fluorinated catalyst with a fluorine purge stream comprising (or consisting essentially of, or consisting of) any inert gas disclosed in this document, for example, nitrogen.

[0278] Aspect 77. The method defined in any of the preceding aspects, wherein the fluorine purge stream is substantially free of oxygen-containing compounds, for example, less than about 100 Petition 870250083407, dated 09 / 16 / 2025, pages 280 / 309 79 / 91 ppmw.

[0279] Aspect 78. The method defined in any of the preceding aspects, wherein the fluorine purge stream is substantially free of halogen-containing compounds (substantially halogen-free), for example, less than about 100 ppmw.

[0280] Aspect 79. The method defined in any of the preceding aspects, wherein the fluoride purging step is conducted at a fluoride purging temperature in any fluoride purging temperature range disclosed in this document, for example, from about 0°C to about 500°C, from about 0°C to about 400°C, from about 15°C to about 475°C, from about 15°C to about 300°C, or from about 25°C to about 250°C, or from about 25°C to about 450°C, such as about 450°C.

[0281] Aspect 80. The method defined in any of the preceding aspects, wherein the fluoride purging step is conducted for a period of time in any range of fluoride purging time periods disclosed in this document, for example, from about 0.25 hours to about 72 hours, or from about 1 hour to about 48 hours.

[0282] Aspect 81. The method defined in any of the preceding aspects, wherein the fluoride purging step is carried out for a period of time sufficient to reduce the fluoride content of the outgoing fluoride purge effluent stream, after contact of the coke-free and fluorinated catalyst, to less than any maximum fluoride content described herein, for example, less than about 100 ppmw of fluoride-containing compounds.

[0283] Aspect 82. The method defined in any of the preceding aspects, wherein the method further comprises an oxygen purge step after the carbon burning step or a fluorine purge step, the oxygen purge step comprising contacting the catalyst with an oxygen purge stream comprising (or consisting essentially of, or consisting of) any inert gas disclosed in this document, for example, nitrogen. Petition 870250083407, dated 09 / 16 / 2025, pages 281 / 309 80 / 91

[0284] Aspect 83. The method defined in any of the preceding aspects, wherein the oxygen purge stream is substantially free of oxygen-containing compounds, for example, less than about 100 ppmw.

[0285] Aspect 84. The method defined in any of the preceding aspects, wherein the oxygen purge stream is substantially free of halogen-containing compounds (substantially halogen-free), for example, less than about 100 ppmw.

[0286] Aspect 85. The method defined in any of the preceding aspects, wherein the oxygen purge step is conducted at an oxygen purge temperature in any oxygen purge temperature range disclosed in this document, for example, from about 0°C to about 400°C, from about 15°C to about 350°C, from about 25°C to about 325°C, from about 25°C to about 300°C, from about 15°C to about 300°C, from about 25°C to about 260°C, from about 25°C to about 250°C, from about 0°C to about 600°C, from about 15°C to about 550°C, from about 25°C to about 500°C, or from about 25°C to approximately 450°C.

[0287] Aspect 86. The method defined in any of the preceding aspects, wherein the oxygen purge step is conducted for a period of time in any range of oxygen purge time periods disclosed in this document, for example, from about 0.5 hours to about 96 hours, or from about 1 to about 48 hours.

[0288] Aspect 87. The method defined in any of the preceding aspects, wherein the oxygen purge step is conducted for a period of time sufficient to reduce the oxygen content of the outgoing oxygen purge effluent stream, after contact with the catalyst, to less than any maximum oxygen content described in this document, for example, less than about 100 ppmw of oxygen-containing compounds.

[0289] Aspect 88. The method defined in any of the preceding aspects, wherein the method further comprises a step of Petition 870250083407, dated 09 / 16 / 2025, pages 282 / 309 81 / 91 hydrocarbon treatment prior to the carbon combustion stage, the hydrocarbon treatment stage comprising the contact of the spent chlorinated catalyst with a hydrocarbon treatment stream comprising a hydrocarbon feed.

[0290] Aspect 89. The method defined in any of the above aspects, wherein the hydrocarbon feed comprises (or consists essentially of, or consists of) C6-C8 alkanes and / or cycloalkanes.

[0291] Aspect 90. The method defined in any of the preceding aspects, wherein the hydrocarbon treatment step is conducted at a hydrocarbon treatment temperature in any hydrocarbon treatment temperature range disclosed in this document, for example, from about 400°C to about 600°C.

[0292] Aspect 91. The method defined in any of the preceding aspects, wherein the hydrocarbon treatment step is conducted for a period of time in any range of hydrocarbon treatment time periods disclosed in this document, for example, from about 1 to about 48 hours.

[0293] Aspect 92. The method defined in any of the above aspects, wherein the method further comprises a reduction step after the fluorination step.

[0294] Aspect 93. The method defined in any of the preceding aspects, wherein the reduction step comprises contacting the regenerated catalyst, the spent fluorinated catalyst or the decoked and fluorinated catalyst with a reducing gas stream comprising (or consisting essentially of, or consisting of) molecular hydrogen.

[0295] Aspect 94. The method defined in any of the above aspects, wherein the reduction of spent fluorinated catalyst or regenerated catalyst occurs at a temperature of about 600°F to about 1,200°F, about 700°F to about 1,100°F, about 800°F to about 1,000°F, about 900°F to about 1,000°F or about 950°F to about 1,000°F. Petition 870250083407, dated 09 / 16 / 2025, pp. 283 / 309 82 / 91

[0296] Aspect 95. The method defined in any of the preceding aspects, wherein the reduction of spent fluorinated catalyst or regenerated catalyst occurs, at least partially, in an atmosphere comprising (consisting essentially of, or consisting of) an inert gas (such as nitrogen), hydrogen (H2) or a combination thereof; wherein optionally the volume ratio of the inert gas to hydrogen (H2) is about 10:90 to about 90:10, about 20:80 to about 80:20 or about 40:60 to about 60:40.

[0297] Aspect 96. The method defined in any of the preceding aspects, wherein the reducing gas stream comprises a molar % of molecular hydrogen greater than any minimum amount or in any range disclosed in this document, for example, greater than about 25 molar % or greater than about 75 molar %.

[0298] Aspect 97. The method defined in any of the preceding aspects, wherein the reduction step is conducted at a peak reduction temperature in any peak reduction temperature range disclosed in this document, for example, from about 200°C to about 600°C, or from about 400°C to about 600°C.

[0299] Aspect 98. The method defined in any of the preceding aspects, wherein the reduction step is initiated at an initial reduction temperature which is the same as any oxygen purge temperature disclosed in this document, for example, in a range of about 0°C to about 600°C, about 15°C to about 550°C, about 25°C to about 500°C, about 25°C to about 450°C, about 0°C to about 500°C, about 0°C to about 300°C, about 20°C to about 250°C, or about 15°C to about 50°C.

[0300] Aspect 99. The method defined in any of the preceding aspects, wherein the reduction step is conducted for a period of time in any range of reduction step time periods disclosed in this document, for example, from about 0.5 hours to about 48 hours, of Petition 870250083407, dated 09 / 16 / 2025, pp. 284 / 309 83 / 91 about 10 to about 30 hours.

[0301] Aspect 100. The method defined in any of the preceding aspects, wherein the catalyst support comprises (or essentially consists of, or consists of) a zeolite, an amorphous inorganic oxide or any combination thereof.

[0302] Aspect 101. The method defined in any of the preceding aspects, wherein the catalyst support comprises (or essentially consists of, or consists of) an L-zeolite, a Y-zeolite, a mordenite, an omega zeolite and / or a beta zeolite.

[0303] Aspect 102. The method defined in any of the preceding aspects, wherein the catalyst support comprises (or essentially consists of, or consists of) a potassium L-zeolite or a barium ion-exchanged L-zeolite.

[0304] Aspect 103. The method defined in any of the above aspects, wherein the catalyst support comprises (or essentially consists of, or consists of) a binder comprising alumina, silica, a mixed oxide thereof or a mixture thereof.

[0305] Aspect 104. The method defined in any of the above aspects, wherein the transition metal comprises a Group 8-11 transition metal.

[0306] Aspect 105. The method defined in any of the above aspects, wherein the transition metal comprises (or consists essentially of, or consists of) platinum.

[0307] Aspect 106. The method defined in any of the preceding aspects, wherein the catalyst comprises any percentage range by weight of transition metal disclosed in this document, for example, from about 0.1% by weight to about 10% by weight, or from about 0.3% by weight to about 5% by weight of transition metal.

[0308] Aspect 107. The method defined in any of the aspects above, wherein the spent catalyst comprises any range Petition 870250083407, dated 09 / 16 / 2025, pp. 285 / 309 84 / 91 percentage by weight of platinum disclosed in this document, for example, from about 0.1% by weight to about 10% by weight, or from about 0.5% by weight to about 2% by weight of platinum.

[0309] Aspect 108. The method defined in any of the preceding aspects, wherein the catalyst comprises (or consists essentially of, or consists of) platinum in a KL zeolite.

[0310] Aspect 109. The method defined in any of the preceding aspects, wherein the catalyst further comprises chlorine and fluorine.

[0311] Aspect 110. The method defined in any of the preceding aspects, wherein the catalyst comprises any range of chlorine percentage by weight and / or range of fluorine percentage by weight disclosed in this document, for example, from about 0.01% by weight to about 5% by weight, or from about 0.3% to about 1.3% by weight of fluorine, and / or from about 0.01% by weight to about 5% by weight, from about 0.3% by weight to about 3% by weight, or from about 0.3% to about 1.3% by weight of chlorine.

[0312] Aspect 111. The method defined in any of the preceding aspects, wherein the catalyst comprises any molar ratio of chlorine:fluorine disclosed in this document, for example, from about 0.5:1 to about 4:1.

[0313] Aspect 112. The method defined in any of the preceding aspects, wherein the chlorine-containing compound comprises (or essentially consists of, or consists of) hydrochloric acid, chlorine gas (Cl2), carbon tetrachloride, tetrachloroethylene, chlorobenzene, methyl chloride, methylene chloride, chloroform, allyl chloride, trichloroethylene, a chloramine, a chlorine oxide, a chlorine acid, chlorine dioxide, dichloride monoxide, dichloride heptoxide, chloric acid, perchloric acid, ammonium chloride, tetramethylammonium chloride, tetraethylammonium chloride, tetrapropylammonium chloride, tetrabutylammonium chloride, methyltriethylammonium chloride or any combination thereof.

[0314] Aspect 113. The method defined in any of the Petition 870250083407, dated 09 / 16 / 2025, pages 286 / 309 85 / 91 previous aspects, where the chlorine-containing compound comprises (or consists essentially of, or consists of) chlorine gas (Cl2).

[0315] Aspect 114. A reactivated catalyst or a regenerated catalyst produced by the method defined in any of the preceding aspects.

[0316] Aspect 115. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst comprises any amount of iron disclosed herein, for example, less than about 400 ppmw, less than about 300 ppmw, less than about 250 ppmw, from about 5 ppmw to about 400 ppmw, from about 50 ppmw to about 300 ppmw, or from about 50 ppmw to about 250 ppmw of iron.

[0317] Aspect 116. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst comprises any amount of carbon disclosed herein, for example, less than about 1% by weight, less than about 0.5% by weight, from about 0.01% by weight to about 1% by weight, from about 0.01% by weight to about 0.75% by weight, from about 0.01% by weight to about 0.5% by weight, or from about 0.02% by weight to about 0.5% by weight of carbon.

[0318] Aspect 117. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst comprises any amount of chlorine disclosed in this document, for example, from about 0.01% by weight to about 5% by weight, from about 0.05% by weight to about 3% by weight, from about 0.05% by weight to about 2.0% by weight, or from about 0.3% by weight to about 1.3% by weight of chlorine.

[0319] Aspect 118. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst comprises any Petition 870250083407, dated 09 / 16 / 2025, pages 287 / 309 86 / 91 quantity of fluoride disclosed in this document, for example, from about 0.01% by weight to about 5% by weight, from about 0.05% by weight to about 3% by weight, from about 0.01% by weight to about 3% by weight, from about 0.1% by weight to about 1.3% by weight, or from about 0.15% by weight to about 1.3% by weight of fluoride.

[0320] Aspect 119. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst is characterized by a CONTENT within about 50°F, within about 40°F, within about 30°F, or within about 20°F, of the CONTENT of a fresh reference catalyst.

[0321] Aspect 120. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst is characterized by a TSOR within about 50°F, within about 40°F, within about 30°F, or within about 20°F, of the TSOR of a fresh reference catalyst.

[0322] Aspect 121. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst is characterized by a fouling rate (FR) in any range disclosed in this document, for example, from about 0.01° F / ha to about 0.25° F / h, from about 0.02° F / ha to about 0.2° F / h, from about 0.03° F / ha to about 0.2° F / h, or from about 0.03° F / ha to about 0.15° F / h.

[0323] Aspect 122. The reactivated catalyst or regenerated catalyst defined in any of the preceding aspects, wherein the reactivated catalyst or regenerated catalyst is characterized by a benzene+toluene selectivity in any selectivity range disclosed in this document, for example, from about 0.88 to about 0.95, or from about 0.89 to about 0.94; or greater than 0.88, or greater than 0.90.

[0324] Aspect 123. The method or catalyst defined in any of the above aspects, wherein the metal reactor (or reactor system of Petition 870250083407, dated 09 / 16 / 2025, pp. 288 / 309 87 / 91 metal) comprises (or consists essentially of, or consists of) stainless steel, for example, 347SS or 321SS.

[0325] Aspect 124. The method or catalyst defined in any of the preceding aspects, further comprising, essentially consisting of, or consisting of recovering at least a portion of the fluorine-containing stream to produce a recovered fluorine-containing stream, wherein, optionally, the recovery occurs after contact of the coke-free catalyst with the fluorine-containing stream; and contacting the coke-free catalyst with the recovered fluorine-containing stream.

[0326] Aspect 125. The method or catalyst defined in any of the preceding aspects, wherein a fluorine concentration in the regenerated catalyst is from about 0.15% by weight to about 1.2% by weight, or from about 0.2% by weight to about 1.2% by weight.

[0327] Aspect 126. The method or catalyst defined in any of the preceding aspects, wherein a fluorine concentration gradient in a regenerated catalyst is 60% or less, 50% or less, 40% or less, 30% or less, 20% or less, or 10% or less.

[0328] Aspect 127. A method of producing a product, the method comprising, consisting essentially of, or consisting of: (A) providing a reactivated or regenerated catalyst, such as any of the preceding aspects, and (B) contacting a hydrocarbon and the reactivated / regenerated catalyst to produce a product, such as an aromatic product.

[0329] Aspect 128. The method defined in any of the preceding aspects, wherein the contact of the hydrocarbon and the reactivated / regenerated catalyst occurs for an effective time to produce a second spent catalyst, and the method further comprises subjecting the second spent catalyst to the method defined in any of the preceding aspects.

[0330] Aspect 129. (I) A method of contacting a spent catalyst with a fluorine-containing stream, or (II) The method defined in either of the preceding aspects, wherein the spent catalyst, such as the Petition 870250083407, dated 09 / 16 / 2025, pages 289 / 309 88 / 91 spent catalyst redistributed, with a fluorine-containing stream, comprises, essentially consists of, or consists of

[0331] (a) providing two or more reactors in fluid communication with each other, wherein the two or more reactors (for example, 2 to 10 reactors, or more) are connected in a series, thus enabling a fluorine-containing stream to be (i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to a first of the two or more reactors and, optionally, (iv) sequentially recirculated through each of the two or more reactors, wherein each of the two or more reactors includes a reservoir in which the spent catalyst is disposed;

[0332] (b) heating one of the two or more reactors to a temperature equal to or greater than a fluorination temperature and maintaining each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature, where the fluorination temperature is effective to decompose at least partially a fluorine-containing compound from the fluorine-containing stream; and

[0333] (c) inject the fluorinated stream and circulate or recirculate the fluorinated stream for an effective time to achieve a desired level of fluorination of the spent catalyst in one of two or more reactors at a temperature that is equal to or greater than the fluorination temperature.

[0334] Aspect 130. The method defined in any of the above aspects, further comprising, consisting essentially of, or consisting of:

[0335] (d) heating one of the two or more reactors to a temperature that is equal to or greater than the fluorination temperature and maintaining each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature; and

[0336] (e) inject the fluoride-containing stream and circulate or recirculate the fluoride-containing stream for an effective time to achieve a desired level of Petition 870250083407, dated 09 / 16 / 2025, pp. 290 / 309 89 / 91 Fluorination of the spent catalyst in two or more reactors at a temperature equal to or greater than the fluorination temperature.

[0337] Aspect 131. The method defined in any of the aspects above, further comprising repeating steps (d) and (e) until the catalyst spent in each of the one or more reactors is fluorinated to a desired level.

[0338] Aspect 132. The method defined in any of the aspects above, where the temperature which is equal to or greater than the fluorination temperature is at least 650°F, or at least 700°F.

[0339] Aspect 133. The method defined in any of the above aspects, wherein the temperature which is equal to or greater than the fluorination temperature is from about 650°F to about 850°F, from about 700°F to about 850°F, from about 700°F to about 800°F, from about 700°F to about 775°F, or from about 700°F to about 750°F.

[0340] Aspect 134. The method defined in any of the above aspects, wherein the temperature which is lower than the fluorination temperature is about 600°F or less.

[0341] Aspect 135. The method defined in any of the above aspects, wherein the temperature which is lower than the fluorination temperature is from about 300°F to about 600°F, from about 400°F to about 600°F or from about 500°F to about 600°F.

[0342] Aspect 136. The method defined in any of the preceding aspects, in which the injection of the fluorine-containing stream comprises, consists essentially of, or consists of:

[0343] (1) select the injection point from one or more injection points, wherein, optionally, the selected injection point is upstream of a reactor (or the reactor different) heated to a temperature that is equal to or greater than the fluorination temperature, and

[0344] (2) inject the fluorine-containing stream into the selected injection joint from one or more injection points. Petition 870250083407, dated 09 / 16 / 2025, pages 291 / 309 90 / 91

[0345] Aspect 137. The method defined in any of the preceding aspects, wherein an amount of the fluorine-containing compound or of the fluorine-containing stream that is injected and circulated / recirculated is effective in placing on the spent catalyst about 0.1% by weight to about 1.5% by weight, about 0.5% by weight to about 1.5% by weight of fluorine, or about 0.15% by weight to about 1.2% by weight of fluorine.

[0346] Aspect 138. The method defined in any of the preceding aspects, further comprising, essentially consisting of, or consisting of analyzing the fluoride-containing stream during circulation or recirculation of the fluoride-containing stream to determine an amount or concentration of the fluoride-containing compound and / or fluoride in the fluoride-containing stream.

[0347] Aspect 139. The method defined in any of the preceding aspects, further comprising, essentially consisting of, or consisting of stopping the circulation / recirculation of the fluorine-containing stream when the amount or concentration of the fluorine-containing compound and / or fluorine is at or below a limit concentration or amount that indicates successful fluorine deposition on the spent catalyst.

[0348] Aspect 140. System for fluorinating a spent catalyst, the system characterized in that it comprises, consists essentially of, or consists of:

[0349] (a) two or more reactors in fluid communication with each other, wherein the two or more reactors are connected in series, thus allowing a fluid stream, such as a stream containing fluorine, to be (i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to a first of the two or more reactors and, optionally, (iv) sequentially recirculated through each of the two or more reactors; and

[0350] (b) two or more heating devices configured to heat each of the two or more reactors to equal temperatures or Petition 870250083407, dated 09 / 16 / 2025, pages 292 / 309 91 / 91 different.

[0351] Aspect 141. The system of Aspect 140, wherein the system comprises at least one injection point for each reactor.

[0352] Aspect 142. The system of Aspect 141, in which at least one injection point is positioned to allow a stream containing fluorine to be injected immediately upstream of any two or more reactors. Petition 870250083407, dated 09 / 16 / 2025, pp. 293 / 309

Claims

1 / 10 CLAIMS 1. A method for regenerating a spent catalyst, characterized by comprising a transition metal and a catalyst support in a metal reactor, the method comprising: (1) contacting the spent catalyst with hydrogen gas to produce a spent catalyst removed; (2) subjecting the removed spent catalyst to a carbon burn at a temperature not exceeding about 500°F to produce a treated spent catalyst; (3) contacting the treated spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst; (4) subjecting the spent chlorinated catalyst to a carbon burn at a temperature not exceeding 900°F, for a time effective to improve a dispersion of the transition metal in the spent chlorinated catalyst to form a redistributed spent catalyst; and (5) contacting the redistributed spent catalyst with a fluorine-containing stream comprising a fluorine-containing compound to form a regenerated catalyst; and (6) reducing the regenerated catalyst.

2. Method according to claim 1, characterized in that the fluorine-containing compound comprises a compound of formula (I): Formula CaHbClcFd (I), where a is 1 to 6, b is 0 to 14, c is 0 to 14, d and e is 1 to 14, where optionally (i) b is not 0, (ii) c is not 0, or (iii) a combination thereof, and Petition 870250083407, 09 / 16 / 2025, p. 294 / 309 2 / 10 where b + c + d = 2a + 2.

3. Method according to claim 1, characterized in that the fluorine-containing compound consists of 1,1,1,2-tetrafluoroethane.

4. Method according to claim 1,5. Method according to claim 1, characterized in that the fluorine-containing compound consists of difluoromethane.

6. Method according to claim 1, characterized in that the fluorine-containing compound consists of dichlorodifluoromethane.

7. Method according to claim 6, characterized in that the fluorine-containing compound further comprises an inert gas, oxygen (O2), or a combination thereof.

8. Method according to claim 6, characterized in that the volume ratio of the inert gas to oxygen (O2) in the fluorine-containing stream is from about 95:5 to about 99:1 (inert gas: oxygen (O2)).

8. Method according to claim 1, characterized by (i) an amount of the fluorine-containing compound in the fluorine-containing stream, (ii) a duration of contact of the redistributed spent catalyst with the fluorine-containing stream, or (iii) a combination thereof is selected to place in the redistributed spent catalyst about 0.15% by weight to about 1.2% by weight of fluorine.

9. Method according to claim 1,characterized by the fluorine-containing stream being substantially free of (i) oxygen-containing compounds, (ii) chlorine-containing compounds that do not include a fluorine atom, or (iii) oxygen-containing compounds and chlorine-containing compounds that do not include a fluorine atom.

10. Method according to claim 1, characterized in that the carbon burn-off temperature of the removed spent catalyst is about 400°F to about 500°F, and the carbon burn-off of the removed catalyst occurs for a time of about 1 minute to about 24 hours.

11. Method according to claim 1, characterized in that an initial amount of a hydrocarbon feed and an amount Petition 870250083407, dated 09 / 16 / 2025,Page 295 / 309 3 / 10 initial amount of an aromatic product is present in the spent catalyst, and the carbon burn-off of the removed spent catalyst removes at least 90% by weight of the initial amount of hydrocarbon feed and at least 90% by weight of the initial amount of aromatic product from the removed spent catalyst.

12. Method according to claim 1, characterized in that a quantity of soft coke is absorbed and / or adsorbed onto the spent catalyst, and the carbon burn-off of the removed spent catalyst reduces the amount of soft coke absorbed and / or adsorbed onto the spent catalyst.

13. Method according to claim 1, characterized in that the temperature of the carbon burn-off of the chlorinated spent catalyst is from about 700°F to about 1,000°F, and the carbon burn-off of the chlorinated spent catalyst occurs for a time from about 1 minute to about 24 hours.

14. Method according to claim 1,14. A method characterized by the carbon burn-off of the chlorinated catalyst improving the dispersion of the transition metal in the spent chlorinated catalyst by at least 70%.

15. A method according to claim 1, characterized in that the reduction of the regenerated catalyst occurs at a temperature of about 800°F to about 1000°F.

16. A method according to claim 1, characterized in that the reduction of the regenerated catalyst occurs, at least partially, in an atmosphere comprising an inert gas, hydrogen (H2), or a combination thereof.

17. A method according to claim 16, characterized in that the volume ratio of the inert gas to hydrogen (H2) is about 20:80 to about 80:

20.

18. A method according to claim 1, characterized by further comprising contacting a hydrocarbon feed with an aromatization catalyst under reforming conditions to produce an aromatic product.in which the contact of the hydrocarbon feed and the flavoring catalyst occurs for a period of time sufficient to form the spent catalyst.

19. Method according to claim 1, characterized in that each of the steps (1) to (6) is carried out in the metal reactor.

20. Method according to claim 19, characterized in that the metal reactor is made of stainless steel.

21. A method for contacting a spent catalyst with a fluorine-containing stream, the method characterized by comprising: (a) providing two or more reactors in fluid communication with each other, wherein the two or more reactors are connected in a series, thus enabling a fluorine-containing stream to be (i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to one of the first two or more reactors and,Optionally, (iv) sequentially recirculated through each of two or more reactors, wherein each of the two or more reactors includes a reservoir in which the spent catalyst is disposed; (b) heating one of the two or more reactors to a temperature equal to or greater than a fluorination temperature and maintaining each of the remaining reactors of the two or more reactors at a temperature below the fluorination temperature, where the fluorination temperature is effective to at least partially decompose a fluorine-containing compound from the fluorine-containing stream; and (c) injecting the fluorine-containing stream and circulating or recirculating the fluorine-containing stream for an effective time to achieve a desired level of fluorination of the spent catalyst in one of the two or more reactors at a temperature that is equal to or greater than the fluorination temperature.

22. Method according to claim 21,characterized by further comprising: (d) heating one different of the two or more reactors to a temperature that is equal to or greater than the fluorination temperature and maintaining each of the remaining reactors of the two or more reactors at a temperature lower than the fluorination temperature; and (e) injecting the fluorinated stream and circulating or recirculating the fluorinated stream for an effective time to achieve a desired level of fluorination of the spent catalyst in the different of the two or more reactors at a temperature that is equal to or greater than the fluorination temperature.

23. Method according to claim 22, characterized by further comprising repeating steps (d) and (e) until the spent catalyst in each of the one or more reactors is fluorinated to a desired level.

24. Method according to any one of claims 21 to 23,24. A method, characterized by a temperature that is equal to or greater than the fluorination temperature of at least 650°F, and a temperature that is less than the fluorination temperature of about 600°F or less.

25. A method, according to any one of claims 21 to 23, characterized by a temperature that is equal to or greater than the fluorination temperature of about 650°F to about 850°F.

26. A method, according to any one of claims 21 to 23, characterized by a temperature that is equal to or greater than the fluorination temperature of about 700°F to about 850°F.

27. A method, according to any one of claims 21 to 23, characterized by a temperature that is less than the fluorination temperature of about 300°F to about 600°F.

28. A method according to any one of claims 21 to 23, characterized by the injection of a fluorine-containing stream, comprises: (1) selecting the injection point from one or more injection points,(2) injecting the fluorine-containing stream into the selected injection junction from one or more injection points.

29. Method according to claim 28, characterized in that the selected injection point is upstream of a reactor or the reactor is heated to a temperature that is equal to or greater than the fluorination temperature.

30. Method according to any one of claims 21 to 23, characterized in that an amount of the fluorine-containing compound or fluorine-containing stream that is injected and circulated / recirculated is effective in placing on the spent catalyst about 0.1% by weight to about 1.5% by weight of fluorine.

31. Method, according to any one of claims 21 to 23, characterized in that an amount of the fluorine-containing compound or fluorine-containing stream that is injected and circulated / recirculated is effective in placing on the spent catalyst about 0.15% by weight to about 1.2% by weight of fluorine.

32. Method,32. A method according to any one of claims 21 to 23, characterized by further comprising analyzing the fluorine-containing stream during circulation or recirculation of the fluorine-containing stream to determine an amount or concentration of the fluorine-containing compound and / or fluorine in the fluorine-containing stream.

33. A method according to any one of claims 21 to 23, characterized by further comprising stopping the circulation / recirculation of the fluorine-containing stream when the amount or concentration of the fluorine-containing compound and / or fluorine is equal to or less than a limiting concentration or amount indicating successful fluorine deposition on the spent catalyst.

34. A system for fluorinating a spent catalyst, the system characterized by comprising: (a) two or more reactors in fluid communication with each other, wherein the two or more reactors are connected in series, thus allowing a fluid stream, such as a fluorine-containing stream,(i) injected at a selected injection point from one or more injection points, (ii) sequentially circulated through each of the two or more reactors downstream of the injection point, (iii) returned to a first of the two or more reactors and, optionally, (iv) sequentially recirculated through each of the two or more reactors; and (b) two or more heating devices configured to heat each of the two or more reactors to equal or different temperatures.

35. System according to claim 34, characterized in that the system includes exactly two reactors, three reactors, four reactors, five reactors, six reactors, seven reactors, eight reactors, nine reactors or ten reactors.

36. System according to claim 34, characterized in that the two or more heating devices comprise two or more tube furnaces.

37. System according to claim 34,characterized by one or more injection points comprising at least one injection point for each of two or more reactors.

38. System according to claim 37, characterized in that the system includes exactly two, three, four, five, six, seven, eight, nine or ten reactors and at least two, three, four, five, six, seven, eight, nine or ten injection points, respectively.

39. System according to claim 34, characterized by further comprising the spent catalyst, wherein the spent catalyst is disposed in at least one of two or more reactors and the spent catalyst comprises a transition metal and a catalyst support.

40. System according to claim 34, characterized by the two or more reactors comprising two or more metal reactors.

41. Method of regenerating a spent catalyst, characterized in that it comprises a transition metal and a catalyst support in a metal reactor.the method comprising: (1) contacting the spent catalyst with a chlorine-containing stream comprising a chlorine-containing compound to produce a chlorinated spent catalyst; (2) contacting the chlorinated spent catalyst with a decoking gas stream comprising oxygen to produce a decoked catalyst; and Petition 870250083407, dated 09 / 16 / 2025, page 300 / 309 8 / 10 (3) contacting the coke-free catalyst with a fluorine-containing stream comprising a fluorine-containing compound to produce a regenerated catalyst, wherein the fluorine-containing compound comprises a hydrofluorocarbon (HFC), a chlorofluorocarbon (CFC), a hydrochlorofluorocarbon (HCFC) or a combination thereof.

42. Method according to claim 41, characterized by the fluorine-containing compound comprising a compound of formula (I): CaHbClcFd Formula (I), wherein - a is from 1 to 6, b is 0 to 14, c is 0 to 14, d and e is 1 to 14, wherein, optionally, (i) b is not 0, (ii) c is not 0, or (iii) a combination thereof,and where b + c + d = 2a + 2.

43. Method according to claim 42, characterized in that b is not 0.

44. Method according to claim 42, characterized in that c is not 0.

45. Method according to claim 41, characterized in that the fluorine-containing compound comprises 1,1,1,2-tetrafluoroethane.

46. Method according to claim 41, characterized in that the fluorine-containing compound comprises dichlorodifluoromethane, difluoromethane or a combination thereof.

47. Method according to claim 41, characterized in that the fluorine-containing stream further comprises an inert gas, air or a combination thereof.

48. Method according to claim 41, characterized in that the fluorine-containing stream further comprises an inert gas and air at a ratio of Petition 870250083407, dated 16 / 09 / 2025, p. 301 / 309 9 / 10 volume of about 3:1 to about 5:1 (inert gas:air).

49. Method according to claim 41,characterized in that the fluorine-containing compound is present in the fluorine-containing stream in an amount effective to impart a fluorine [F] concentration in the fluorine-containing stream of about 0.05% by weight to about 3% by weight.

50. Method according to claim 41, characterized in that the fluorine-containing stream is substantially free of oxygen-containing compounds, chlorine-containing compounds that do not include a fluorine atom, or oxygen-containing compounds and chlorine-containing compounds that do not include a fluorine atom.

51. Method according to claim 41, characterized in that contact of the coke-free catalyst with the fluorine-containing stream occurs at a temperature of about 0°C to about 500°C.

52. Method according to claim 41, characterized in that contact of the coke-free catalyst with the fluorine-containing stream occurs at a pressure of about 0.5 bar to about 7 bar.

53. Method according to claim 41,characterized by the contact of the coke-free catalyst with the fluorine-containing stream occurring for a period of time of about 0.5 to about 96 hours.

54. Method, according to claim 41, characterized by further comprising: recovering at least a portion of the fluorine-containing stream to produce a recovered fluorine-containing stream, wherein the recovery occurs after contact of the coke-free catalyst with the fluorine-containing stream; and contacting the coke-free catalyst with the recovered fluorine-containing stream.

55. Method, according to claim 41, characterized in that a fluorine concentration in the regenerated catalyst is of about 0.03% by weight to about 1.3% by weight.

56. Method, according to claim 41, characterized by a Petition 870250083407, dated 09 / 16 / 2025, p. 302 / 309 10 / 10 The fluorine concentration gradient in the regenerated catalyst is 60% or less.

57. Method according to claim 41,characterized by a fluorine concentration gradient in the regenerated catalyst of 40% or less.

58. Method according to claim 41, characterized in that the chlorine-containing stream is substantially free of oxygen-containing compounds and fluorine-containing compounds.

59. Method according to claim 41, characterized in that the decoking gas is substantially free of water.

60. Method according to claim 41, characterized in that the chlorine-containing stream comprises chlorine gas (Cl2) and nitrogen (N2). Petition 870250083407, dated 09 / 16 / 2025, pp. 303 / 309.

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