Catalyst regeneration process and alkane and / or alkyl aromatic hydrocarbon upgrade process

Abstract

A process for regenerating an at least partially deactivated catalyst, which may include a Group 10 element, an inorganic support, and contaminants. The Group 10 element may have a concentration of 0.001 wt% to 6 wt% based on the weight of the inorganic support. The process includes: (I) adding H 2 The process may include heating the deactivated catalyst with a heated gas mixture containing O to produce a precursor catalyst. 2 providing an oxidative gas comprising O, and (III) contacting the precursor catalyst with the oxidative gas at an oxidation temperature for a duration of at least 30 seconds to produce an oxidized precursor catalyst. The process may also include (IV) obtaining a regenerated catalyst from the oxidized precursor catalyst.

Description

[Technical Field]

[0001] Cross-reference of related applications This application claims priority and benefits of U.S. Provisional Application No. 63 / 195,966, filed 2 June 2021, and U.S. Provisional Application No. 63 / 328,923, filed 8 April 2022, which are incorporated herein by reference in their entirety.

[0002] field This disclosure relates to catalyst regeneration processes and upgrade processes for alkanes and / or alkyl aromatic hydrocarbons. [Background technology]

[0003] background Catalytic dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of alkanes and / or alkyl aromatic hydrocarbons are endothermic, equilibrium-limited, industrially important chemical transformation processes. Alkanes, e.g., C2-C 16 Dehydrogenation of alkanes and / or alkyl aromatic hydrocarbons, such as ethylbenzene, can be carried out via various different supported catalyst systems, such as Pt-based, Cr-based, Ga-based, V-based, Zr-based, In-based, W-based, Mo-based, Zn-based, and Fe-based systems. Among existing propane dehydrogenation processes, a particular process using an alumina-supported chromia catalyst yields one of the highest propylene yields of about 50% (55% propane conversion rate with 90% propylene selectivity), which is achieved at temperatures of about 560°C to 650°C and low pressures of 20 kPa to 50 kPa absolute pressure. To increase the efficiency of the dehydrogenation process, it is desirable to increase the propylene yield without operating at such low pressures.

[0004] Increasing the temperature of the dehydrogenation process is one way to increase the conversion rate of the process according to the thermodynamics of the process. For example, at 670°C and 100 kPa absolute pressure, in the absence of any inert / diluent, the equilibrium propylene yield was estimated by simulation to be approximately 74%. However, at such high temperatures, the catalyst deactivates very rapidly, and / or the propylene selectivity becomes uneconomically low. The rapid deactivation of the catalyst is thought to be due to coke deposition on the catalyst and / or aggregation of the active phase. While the coke can be removed by combustion using an oxygen-containing gas, the aggregation of the active phase is thought to worsen during the combustion process, rapidly reducing the activity and stability of the catalyst. Therefore, there is a need for improved processes for regenerating at least partially deactivated catalysts, as well as improved processes for dehydrogenating, dehydrogenating aromaticating, and / or dehydrogenating cyclizing alkanes and / or alkyl aromatic hydrocarbons. This disclosure satisfies this need and other needs. [Overview of the Initiative]

[0005] overview The present invention provides a process for regenerating at least partially deactivated catalysts and a process for upgrading hydrocarbons. In some embodiments, the process can be used to regenerate at least partially deactivated catalysts which may contain Group 10 elements, an inorganic support, and impurities. The Group 10 elements may be present in concentrations ranging from 0.001 wt% to 6 wt% based on the mass of the inorganic support. The process may include the step of (I) heating the at least partially deactivated catalyst with a heating gas mixture which may contain H2O at a concentration of more than 5 mol% based on its total moles to produce a precursor catalyst. The process may also include the step of (II) supplying an oxidative gas which may contain 5 mol% or less of H2O based on its total moles. The process may also include the step of (III) contacting the precursor catalyst with the oxidative gas at an oxidation temperature ranging from 620°C to 1,000°C for a duration of at least 30 seconds, preferably at least 1 minute, preferably at least 5 minutes to produce an oxidized precursor catalyst. The process may also include the step of (IV) obtaining a regenerated catalyst from the oxidized precursor catalyst.

[0006] In other embodiments, the hydrocarbon upgrading process may include the step of (I) contacting a hydrocarbon-containing feed with a catalyst which may include a Group 10 element and an inorganic support to cause one or more of the hydrocarbon-containing feed to undergo dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization, thereby producing at least a partially deactivated catalyst which may include a Group 10 element, an inorganic support, and impurities, and an effluent which may include one or more upgraded hydrocarbons and molecular hydrogen. The hydrocarbon-containing feed may include one or more C2-C 16 Straight-chain or branched alkanes, or one or more C4-C 16 Cyclic alkanes, one or more C8-C 16The catalyst may contain alkyl aromatic hydrocarbons or mixtures thereof. Group 10 elements may be present in concentrations ranging from 0.001 wt% to 6 wt% based on the mass of the inorganic support. The hydrocarbon-containing feed and catalyst may be contacted at temperatures ranging from 300°C to 900°C. One or more upgraded hydrocarbons may include at least one of dehydrogenated hydrocarbons, dehydrogenated aromatic hydrocarbons, and dehydrogenated cyclized hydrocarbons. The process may also include the step of (II) heating a partially deactivated catalyst with a heating gas mixture which may contain H2O at a concentration of more than 5 mol% based on its total moles to produce a precursor catalyst. The process may also include the step of (III) supplying an oxidizing gas which may contain 5 mol% or less of H2O based on its total moles. The process may also include the step of (IV) contacting the precursor catalyst with the oxidizing gas at an oxidation temperature ranging from 620°C to 1,000°C for a duration of at least 30 seconds to produce an oxidized precursor catalyst. The process may also include the step of (V) obtaining a regenerated catalyst from the oxidized precursor catalyst. The process may also include (VI) contacting an additional amount of hydrocarbon-containing feed with at least a portion of the regenerated catalyst to produce at least partially deactivated catalyst and additional effluent. [Brief explanation of the drawing]

[0007] [Figure 1] This example demonstrates that the catalyst used in Example 6 can be efficiently regenerated over 80+ cycles using a specific two-step regeneration scheme. [Figure 2] The dehydrogenation of isobutane using the catalyst demonstrated that the catalyst remained stable for 30+ cycles despite being exposed to a regeneration temperature of 800°C. [Figure 3] The performance of the catalyst used in Example 19 demonstrates that it remained stable for 30+ cycles despite being exposed to a regeneration temperature of 800°C. [Figure 4] The performance of the primary catalyst used in Example 20 demonstrates that it remained stable over 20+ cycles despite being exposed to a regeneration temperature of 800°C. [Figure 5] The performance of the secondary catalyst used in Example 20 demonstrates that it remained stable for 30+ cycles despite being exposed to a regeneration temperature of 800°C. [Figure 6] The performance of the catalyst used in Example 26 demonstrates that it remained stable for 20+ cycles despite being exposed to a regeneration temperature of 800°C. [Figure 7] The performance of comparative catalyst 1, which remained inactive despite reaching the regeneration temperature (620°C), indicates that it was significantly lower than that of the other examples. [Figure 8] This demonstrates that the catalyst composition (catalyst 33) maintained its performance over 204 cycles. [Modes for carrying out the invention]

[0008] Detailed explanation The following describes various specific embodiments, versions, and examples of the present invention, including preferred embodiments and definitions adopted for the purpose of understanding the claimed invention. While the following detailed description provides specific preferred embodiments, those skilled in the art will see that these embodiments are merely illustrative and that the present invention can be carried out in other ways. For the purpose of determining infringement, the scope of the present invention includes any one or more of the appended claims and their equivalents, elements, or limitations that are equivalent to those listed. Any reference to “invention” may refer to one or more of the present invention as defined by the claims, but not necessarily all of them. This disclosure describes a process that includes at least one “step.” It should be understood that each step is an action or operation that may be performed once or multiple times in a continuous or discontinuous manner within the process. Unless otherwise specified or the context makes it clear that there is another meaning, the steps of the process may be performed sequentially in the order described, with or without overlap with one or more other steps, or in any other order. Furthermore, one or more, or even all, steps may be performed simultaneously with respect to the same or different batches of material. For example, in a continuous process, the first step of the process may be performed with respect to the raw material that was just supplied to the process at the beginning of the process, while the second step is performed simultaneously with respect to intermediate material resulting from the processing of raw material supplied to the process earlier than the first step. Preferably, the steps are performed in the order described.

[0009] Unless otherwise indicated, all numbers indicating quantities in this disclosure should be understood to be modified in all cases by the term “approximately.” Furthermore, the exact numerical values ​​used herein and in the claims should be understood to constitute a particular embodiment. Efforts have been made to ensure the accuracy of the data in the examples. However, it should be understood that all measurement data inherently contain a certain level of error due to the limitations of the techniques and / or equipment used to perform the measurements. This specification uses a set of upper and lower bounds to describe specific embodiments and features. Unless otherwise indicated, it should be understood that we intend ranges that include any pair of values, for example, any pair of lower and upper bounds, any pair of lower bounds, and / or any pair of upper bounds. As used herein, the indefinite articles "a" or "an" mean "at least one" unless the contrary is specified or the context clearly dictates otherwise. Thus, embodiments using "a reactor" or "a conversion zone" include embodiments using one, two, or more than two reactors or conversion zones unless the contrary is specified or the context clearly indicates that only one reactor or conversion zone is used.

[0010] The term "hydrocarbon" means (i) any compound consisting of hydrogen atoms and carbon atoms or (ii) any mixture of two or more such compounds of (i). The term "Cn hydrocarbon" (where n is a positive integer) means (i) any hydrocarbon compound containing a total of n carbon atoms in its molecule or (ii) any mixture of two or more such hydrocarbon compounds of (i). Thus, C2 hydrocarbons can be ethane, ethylene, acetylene, or any mixture of at least two of these compounds in any ratio. "Cm-Cn hydrocarbon" or "Cm~Cn hydrocarbon" (where m and n are positive integers and m < n) means any one of Cm, Cm+1, Cm+2,..., Cn-1, Cn hydrocarbons or any mixture of two or more of these. Thus, "C2-C3 hydrocarbon" or "C2~C3 hydrocarbon" can be any one of ethane, ethylene, acetylene, propane, propene, propyne, propadiene, cyclopropane, and any mixture of two or more of these components in any ratio. "Saturated C2-C3 hydrocarbon" can be any one of ethane, propane, cyclopropane, or any mixture of two or more of these in any ratio. "Cn+ hydrocarbon" means (i) any hydrocarbon compound containing at least n carbon atoms in total in its molecule or (ii) any mixture of two or more such hydrocarbon compounds of (i). "Cn- hydrocarbon" means (i) any hydrocarbon compound containing a maximum of n carbon atoms in total in its molecule or (ii) any mixture of two or more such hydrocarbons of (i). "Cm hydrocarbon stream" means a hydrocarbon stream consisting essentially of Cm hydrocarbons. "Cm-Cn hydrocarbon stream" means a hydrocarbon stream consisting essentially of Cm-Cn hydrocarbons.

[0011] For the purposes of this disclosure, the nomenclature of elements is as defined in Hawley's Condensed Chemical Dictionary, 16 th This disclosure conforms to the version of the periodic table (under the new notation) provided in Ed., John Wiley & Sons, Inc., (2016), Appendix V. For example, Group 2 elements include Mg, Group 8 elements include Fe, Group 9 elements include Co, Group 10 elements include Ni, and Group 13 elements include Al. As used herein, the term “metalloid” refers to the following elements: B, Si, Ge, As, Sb, Te, and At. In this disclosure, when a given element is indicated to exist, it may exist in its elemental state or as any compound thereof, unless otherwise stated or the context makes it clear that it should be interpreted otherwise. The term "alkane" refers to a saturated hydrocarbon. The term "cyclic alkane" refers to a saturated hydrocarbon that contains a cyclic carbon ring in its molecular structure. Alkanes can be linear, branched, or cyclic. The term "aromatic" should be understood in accordance with the scope approved in the relevant art, and includes alkyl-substituted and unsubstituted mononuclear and polynuclear compounds. When used in relation to a device, for example, an outgoing stream obtained from a conversion zone, the term "rich" means that the feed material supplied to the device from which the stream is drawn contains material X at a higher concentration. When used in relation to a device, for example, an outgoing stream obtained from a conversion zone, the term "lean" means that the feed material supplied to the device from which the stream is drawn contains material X at a lower concentration.

[0012] The term "mixed metal oxide" refers to a composition containing oxygen atoms and at least two different metal atoms, which are mixed together on an atomic scale. For example, "mixed Mg / Al metal oxide" is substantially identical to a composition obtained by calcining Mg / Al hydrotalcite having atomically mixed O, Mg, and Al atoms, and having the following general formula. [ka] In the formula, A is a counter anion with negative charge n, x is an integer in the range >0 to <1, and m is ≥0. A material consisting of nm-sized MgO particles and nm-sized Al2O3 particles mixed together is not a mixed metal oxide because the Mg atoms and Al atoms are mixed on an nm scale, not on an atomic scale.

[0013] The term "selectivity" refers to the rate of a particular compound's formation (on a carbon mole basis) in a catalytic reaction. For example, the statement "the alkane hydrocarbon conversion reaction has 100% selectivity for olefin hydrocarbons" means that 100% (on a carbon mole basis) of the alkane hydrocarbons converted in the reaction are converted to olefin hydrocarbons. When used in relation to specific reactants, the term "conversion rate" refers to the amount of reactant consumed in the reaction. For example, when the specific reactant is propane, a 100% conversion rate means that 100% of the propane is consumed in the reaction. In another example, when the specific reactant is propane, if 1 mole of propane is converted to 1 mole of methane and 1 mole of ethylene, the selectivity for methane is 33.3%, and the selectivity for ethylene is 66.7%. The yield (on a carbon mole basis) is the conversion rate multiplied by the selectivity.

[0014] Hydrocarbon Upgrade Process and Catalyst Regeneration Process Hydrocarbon-containing feeds are not limited to, but may include one or more alkane hydrocarbons, such as C2-C 16 Straight-chain or branched alkanes and / or C4-C 16 Cyclic alkanes, and / or one or more alkyl aromatic hydrocarbons, e.g., C8-C16 It can be an alkyl aromatic hydrocarbon or can contain these. In some embodiments, the hydrocarbon-containing feed optionally contains any C2-C in the hydrocarbon-containing feed 16 alkanes and any C8-C 16 Based on the total volume of the alkyl aromatic hydrocarbon, it can contain 0.1 vol% to 50 vol% of steam. In other embodiments, the hydrocarbon-containing feed contains any C2-C in the hydrocarbon-containing feed 16 alkanes and any C8-C 16 Based on the total volume of the alkyl aromatic hydrocarbon, it can contain <0.1 vol% of steam or may be without steam. Contact the hydrocarbon-containing feed with a catalyst containing a Group 10 element, such as Pt, and an inorganic carrier to cause at least one of dehydrogenation, dehydroaromatization, and dehydrocyclization of at least a portion of the hydrocarbon-containing feed, and a Group 10 element, an inorganic carrier, and contaminants, such as coke, to produce at least partially deactivated catalyst and an effluent that can contain one or more upgraded hydrocarbons and molecular hydrogen.

[0015] The one or more upgraded hydrocarbons can be, but are not limited to, one or more dehydrogenated hydrocarbons, one or more dehydroaromatized hydrocarbons, one or more dehydrocyclized hydrocarbons, or mixtures thereof or can contain these. The hydrocarbon-containing feed and the catalyst can be contacted at a temperature in the range of 300°C to 900°C. In some embodiments, the hydrocarbon-containing feed and the catalyst can be contacted for a time of ≤5 hours, ≤4 hours, or ≤3 hours, ≤1 hour, ≤0.5 hour, ≤0.1 hour, ≤3 minutes, ≤1 minute, ≤30 seconds, or ≤0.1 second. In some embodiments, the hydrocarbon-containing feed and the catalyst can be contacted under a hydrocarbon partial pressure of at least 20 kPa absolute pressure. In this case, the hydrocarbon partial pressure is the total partial pressure of any C2-C 16 alkanes and any C8-C 16 alkyl aromatic hydrocarbon. The catalyst can contain 0.001 wt% to 6 wt% of a Group 10 element, such as Pt, based on the mass of the inorganic carrier.

[0016] A precursor catalyst can be obtained from a catalyst that is at least partially deactivated. In some embodiments, the catalyst that is at least partially deactivated may be supplied as a precursor catalyst. In other embodiments, the precursor catalyst can be obtained by heating the catalyst that is at least partially deactivated with a heating gas mixture, which contains H2O at a concentration of more than 5 mol% based on its total moles. In some embodiments, the heating gas mixture may be produced by burning at least a portion of admixtures placed on the catalyst that are at least partially deactivated, e.g., coke and / or residual hydrocarbon-containing feed, with an oxidizing gas. In some embodiments, the heating gas mixture may be produced by burning fuel with an oxidizing gas. In other embodiments, the heating gas mixture may be produced by burning at least a portion of admixtures placed on the catalyst that are at least partially deactivated and fuel with an oxidizing gas. In other embodiments, a heating gas mixture that may contain H2O at a concentration of more than 5 mol% H2O may be supplied with heated air having H2O at a concentration of more than 5 mol% H2O. The fuel may be, but is not limited to, at least one of H2, CO, and hydrocarbons, or may include these. The oxidizing gas may be, but is not limited to, O2, O3, CO, or any mixture thereof, or may include these. In some embodiments, the heated gas mixture may be in contact with a partially deactivated catalyst for durations of <5 minutes, <2 minutes, <1 minute, <30 seconds, <10 seconds, <5 seconds, <1 second, <0.5 seconds, and <0.1 seconds.

[0017] An oxidizing gas can be supplied. The oxidizing gas may include, based on the total moles of the oxidizing gas, 5 mol% or less of H2O, 4.5 mol% or less of H2O, 4 mol% or less of H2O, 3.5 mol% or less of H2O, 3 mol% or less of H2O, 2.5 mol% or less of H2O, 2 mol% or less of H2O, 1.7 mol% or less of H2O, 1.5 mol% or less of H2O, 1.3 mol% or less of H2O, 1 mol% or less of H2O, 0.7 mol% or less of H2O, 0.5 mol% or less of H2O, 0.3 mol% or less of H2O, or 0.1 mol% or less of H2O. The precursor catalyst can be brought into contact with the oxidizing gas, whether the catalyst is supplied as is in its partially deactivated state or whether the catalyst is heated using a heating gas mixture. To our surprise and astoundment, we discovered that contacting the precursor catalyst with an oxidizing gas containing 5 mol% or less of H2O significantly improved the activity and / or selectivity of the regenerated catalyst, regardless of whether the precursor catalyst was supplied as a partially deactivated catalyst or heated using a heated gas mixture to produce the precursor catalyst. While we do not wish to be constrained by theory, it is possible that the H2O present in the oxidizing gas significantly reduces the effectiveness of Pt redispersion, and consequently, the effectiveness of the regenerated catalyst.

[0018] The precursor catalyst can be brought into contact with an oxidizing gas at oxidation temperatures ranging from 620°C, 650°C, 675°C, 700°C, or 750°C to 775°C, 800°C, 850°C, 900°C, 950°C, or 1,000°C to produce an oxidation precursor catalyst. The precursor catalyst can be brought into contact with an oxidizing gas for durations of at least 30 seconds, at least 1 minute, at least 5 minutes, at least 7 minutes, at least 10 minutes, at least 15 minutes, at least 20 minutes, at least 25 minutes, or at least 30 minutes to produce an oxidation precursor catalyst. In some embodiments, the precursor catalyst can be brought into contact with an oxidizing gas for durations ranging from 30 seconds, 1 minute, 5 minutes, or 10 minutes to 30 minutes, 60 minutes, or 120 minutes to produce an oxidation precursor catalyst. In some embodiments, the precursor catalyst and the oxidizing gas can be in contact with each other for durations of ≤2 hours, ≤1 hour, ≤30 minutes, ≤10 minutes, ≤5 minutes, ≤1 minute, ≤30 seconds, ≤10 seconds, ≤5 seconds, or ≤1 second to generate an oxidized precursor catalyst. For example, the precursor catalyst and the oxidizing gas can be in contact with each other for durations ranging from 2 seconds to 2 hours to generate an oxidized precursor catalyst. In some embodiments, the precursor catalyst and the oxidizing gas can be in contact with each other for a duration sufficient to remove ≥50 wt%, ≥75 wt%, or ≥90 wt%, or >99 wt%, of impurities, such as coke placed on the precursor catalyst.

[0019] The precursor catalyst and the oxidizing gas can be contacted under an oxidizing gas partial pressure ranging from 5 kPa absolute pressure, 10 kPa absolute pressure, 20 kPa absolute pressure, 50 kPa absolute pressure, 100 kPa absolute pressure, 300 kPa absolute pressure, 500 kPa absolute pressure, 750 kPa absolute pressure, or from 1,000 kPa absolute pressure to 1,500 kPa absolute pressure, 2,500 kPa absolute pressure, 4,000 kPa absolute pressure, 5,000 kPa absolute pressure, 7,000 kPa absolute pressure, 8,500 kPa absolute pressure, or 10,000 kPa absolute pressure to produce an oxidizing precursor catalyst. In some embodiments, the partial pressure of the oxidizing gas in contact with the precursor catalyst to generate the oxidation precursor catalyst may range from 5 kPa absolute pressure, 10 kPa absolute pressure, 20 kPa absolute pressure, 50 kPa absolute pressure, 100 kPa absolute pressure, 150 kPa absolute pressure, 200 kPa absolute pressure, 250 kPa absolute pressure, or 300 kPa absolute pressure to 500 kPa absolute pressure, 600 kPa absolute pressure, 700 kPa absolute pressure, 800 kPa absolute pressure, 900 kPa absolute pressure, or 1,000 kPa absolute pressure.

[0020] While we do not wish to be constrained by theory, it is conceivable that at least a portion of the Group 10 elements, such as Pt, placed on the precursor catalyst may aggregate compared to the catalyst before contact with the hydrocarbon-containing feed. When at least a portion of the impurities on the precursor catalyst may be combusted during contact with the oxidizing gas, it is conceivable that at least a portion of the Group 10 elements may be redispersed around the inorganic support. Redispersing at least a portion of the aggregated Group 10 elements can increase activity over multiple cycles and improve catalyst stability. In some embodiments, the oxidizing gas is supplied at a temperature below the oxidation temperature, and the oxidizing gas may be preheated to a temperature higher than the temperature of the precursor catalyst before contacting the precursor catalyst with the oxidizing gas at the oxidation temperature. In some embodiments, the oxidizing gas may be preheated by using a radiant / conductive heat source, a heat exchanger, or a combination thereof. In other embodiments, the oxidizing gas, the precursor catalyst, or both the oxidizing gas and the precursor catalyst may be preheated by using a radiant / conductive heat source, a heat exchanger, or a combination thereof. In other words, the precursor catalyst and / or the oxidizing gas may be heated separately and then contacted with each other at the oxidation temperature, or heated to the oxidation temperature in the presence of each other. In some embodiments, the radiant / conductive heat source may be one or more heat sources or include one or more heat sources.

[0021] A regenerated catalyst can be obtained from an oxidation precursor catalyst. In some embodiments, the oxidation precursor catalyst can be supplied as is as a regenerated catalyst. In some embodiments, the oxidation precursor catalyst can optionally be contacted with a first stripping gas that does not contain O2 to produce a stripped oxidation precursor catalyst, from which a regenerated catalyst can be obtained. The first stripping gas is, but is not limited to, CO, CO2, N2, C1-C4 hydrocarbons, H2O, He, Ne, Ar, or a mixture thereof, or may contain these. In some embodiments, the stripped oxidation precursor catalyst can be supplied as is as a regenerated catalyst. In some embodiments, at least a portion of the Group 10 elements in the oxidation precursor catalyst, such as Pt, may be in a higher oxidation state compared to the Group 10 elements in a catalyst contacted with a hydrocarbon-containing feed and to the Group 10 elements in a catalyst that is at least partially deactivated. In some embodiments, the oxidation precursor catalyst or exfoliation oxidation precursor catalyst can be contacted with an H2-containing atmosphere to produce a reduction catalyst. In other embodiments, the oxidation precursor catalyst or exfoliation oxidation precursor catalyst can be contacted with an atmosphere containing H2, CO, CH4, C2H6, C3H8, C2H4, C3H6, water vapor, or a mixture thereof to produce a reduction catalyst. In some embodiments, the atmosphere contacted with the oxidation precursor catalyst may also include an inert gas, such as Ar, Ne, He, N2, CO2, H2O, or a mixture thereof. In these embodiments, at least a portion of the Group 10 elements in the reduction catalyst may be reduced to a lower oxidation state, such as an elemental state, compared to the Group 10 elements in the oxidation precursor catalyst.

[0022] In some embodiments, the oxidation precursor catalyst or the exfoliation oxidation precursor catalyst may be in contact with an H2-containing atmosphere or an atmosphere containing H2, CO, CH4, C2H6, C3H8, C2H4, C3H6, water vapor, or a mixture thereof at temperatures ranging from 400°C, 450°C, 500°C, 550°C, 600°C, 620°C, 650°C, or 670°C to 720°C, 750°C, 800°C, or 900°C. The oxidation precursor catalyst or the exfoliation oxidation precursor catalyst and the H2-containing atmosphere or the atmosphere containing H2, CO, CH4, C2H6, C3H8, C2H4, C3H6, water vapor, or a mixture thereof may be in contact for durations of 0.01 seconds, 0.1 seconds, 1 second, 5 seconds, 10 seconds, 20 seconds, 30 seconds, or 1 minute to 10 minutes, 30 minutes, or 60 minutes. An oxidation precursor catalyst or a delamination oxidation precursor catalyst and an H2-containing atmosphere or an atmosphere containing H2, CO, CH4, C2H6, C3H8, C2H4, C3H6, water vapor, or a mixture thereof may be contacted at a reducing agent partial pressure of 0.1 kPa absolute pressure, 1 kPa absolute pressure, 5 kPa absolute pressure, 10 kPa absolute pressure, 20 kPa absolute pressure, 50 kPa absolute pressure, or 100 kPa absolute pressure, 300 kPa absolute pressure, 500 kPa absolute pressure, 750 kPa absolute pressure, or from 1,000 kPa absolute pressure to 1,500 kPa absolute pressure, 2,500 kPa absolute pressure, 4,000 kPa absolute pressure, 5,000 kPa absolute pressure, 7,000 kPa absolute pressure, 8,500 kPa absolute pressure, or 10,000 kPa absolute pressure. Here, the reducing agent includes H2, CO, CH4, C2H6, C3H8, C2H4, C3H6, and water vapor. In other embodiments, to generate a regenerating catalyst, the partial pressure of the reducing agent may range from 0.1 kPa absolute pressure, 1 kPa absolute pressure, 5 kPa absolute pressure, 10 kPa absolute pressure, 20 kPa absolute pressure, 50 kPa absolute pressure, 100 kPa absolute pressure, 150 kPa absolute pressure, 200 kPa absolute pressure, 250 kPa absolute pressure, or 300 kPa absolute pressure to 500 kPa absolute pressure, 600 kPa absolute pressure, 700 kPa absolute pressure, 800 kPa absolute pressure, 900 kPa absolute pressure, or 1,000 kPa absolute pressure. Here, the reducing agent includes H2, CO, CH4, C2H6, C3H8, C2H4, C3H6, and water vapor.

[0023] In some embodiments, the oxidation precursor catalyst or the exfoliation oxidation precursor catalyst may be contacted with an H2-containing atmosphere at a temperature higher than the operating temperature of the regenerating catalyst. In these embodiments, the reduction catalyst may be cooled to the operating temperature. In some embodiments, the reduction catalyst may be cooled to the operating temperature for durations of 20 minutes or less, 15 minutes or less, 10 minutes or less, 7 minutes or less, 5 minutes or less, 2 minutes or less, 1 minute or less, 30 seconds or less, 10 seconds or less, 5 seconds or less, 2 seconds or less, 1 second or less, 0.1 seconds or less, 0.01 seconds or less, or 0.001 seconds or less. The operating temperature of the catalyst is the temperature at which a hydrocarbon-containing feed or an additional amount of hydrocarbon-containing feed is contacted with the catalyst or regenerating catalyst to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of at least a portion of the hydrocarbon-containing feed, producing at least a partially deactivated catalyst that may contain Group 10 elements, inorganic supports, and impurities, and an effluent that may contain one or more upgraded hydrocarbons and molecular hydrogen. The regenerating catalyst can be obtained from the reducing catalyst. In some embodiments, the reducing catalyst may be supplied directly as the regenerating catalyst. In other embodiments, the reducing catalyst may be contacted with a second stripping gas to produce a regenerating catalyst. The second stripping gas may be, but not limited to, CO, CO2, N2, C1-C4 hydrocarbons, H2O, He, Ne, Ar, or any mixture thereof.

[0024] At least a portion of the regenerated catalyst, new or unused catalyst, or a mixture thereof, can be contacted with an additional amount of hydrocarbon-containing feed in the reaction or conversion zone to produce additional effluent and additional at least partially deactivated catalyst. The cycle time from contact between the hydrocarbon-containing feed and the catalyst to contact between the additional amount of hydrocarbon-containing feed and at least a portion of the regenerated catalyst and optionally the new or unused catalyst may be ≤5 hours, ≤4.5 hours, ≤4 hours, ≤3.5 hours, ≤3 hours, ≤2.5 hours, ≤2 hours, ≤1 hour, ≤0.5 hours, ≤0.2 hours, ≤0.1 hours, ≤0.05 hours, or ≤0.01 hours. The first cycle begins when the catalyst comes into contact with the hydrocarbon-containing feed, and subsequently comes into contact with at least an oxidizing gas to produce an oxidizing precursor catalyst that can be supplied directly as a regenerated catalyst, or comes into contact with at least an oxidizing gas and an optional reducing gas to produce a regenerated catalyst, and the first cycle ends when the regenerated catalyst comes into contact with an additional amount of hydrocarbon-containing feed. If the first stripping gas and / or the second stripping gas or any other stripping gas(s) is used between the hydrocarbon-containing feed and the oxidizing gas flow, between the oxidizing gas and the reducing gas (if used), between the oxidizing gas and the additional amount of hydrocarbon-containing feed flow, and / or between the reducing gas(s) (if used) and the additional amount of hydrocarbon-containing feed flow, the period during which the stripping gas(s) are used will be included in the period included in the cycle time. Therefore, the cycle time from the contact of the hydrocarbon-containing feed and the catalyst in the step to the contact of the additional amount of hydrocarbon-containing feed and the regenerated catalyst may be ≤ 5 hours.

[0025] A catalyst comprising a Group 10 element, such as Pt, and an inorganic support may remain fully active and stable after multiple cycles, for example, at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 100, at least 125, at least 150, at least 175, or at least 200 cycles, with each cycle lasting ≤ 5 hours, ≤ 4 hours, ≤ 3 hours, ≤ 2 hours, ≤ 1 hour, ≤ 50 minutes, ≤ 45 minutes, ≤ 30 minutes, ≤ 15 minutes, ≤ 10 minutes, ≤ 5 minutes, ≤ 1 minute, ≤ 30 seconds, or ≤ 10 seconds. In some embodiments, the cycle time may range from 5 seconds, 30 seconds, 1 minute, or 5 minutes to 10 minutes, 20 minutes, 30 minutes, 45 minutes, 50 minutes, 70 minutes, 2 hours, 3 hours, 4 hours, or 5 hours. In some embodiments, after the catalyst performance has stabilized (the first few cycles may have relatively insufficient or relatively good performance, but the performance can eventually stabilize), the process can yield a first upgraded hydrocarbon product yield, for example, a first propylene yield when the hydrocarbon-containing feed contains propane, of ≥75%, ≥80%, ≥85%, or ≥90%, or >95% of upgraded hydrocarbons, e.g., propylene, with selectivity, upon initial contact with the hydrocarbon-containing feed, and a second upgraded hydrocarbon product yield, of ≥75%, ≥80%, ≥85%, or ≥90%, or >95% of the first upgraded hydrocarbon product yield, of ≥90%, ≥93%, ≥95%, ≥97%, ≥98%, ≥99%, ≥99.5%, or ≥100% of the first upgraded hydrocarbon product yield, upon completion of the last cycle (at least 15 cycles in total).

[0026] In some embodiments, when the hydrocarbon-containing feed contains propane and the upgraded hydrocarbon contains propylene, contact between the hydrocarbon-containing feed and the catalyst composition can result in propylene yields of ≥48%, ≥49%, ≥50%, ≥51%, ≥52%, ≥53%, ≥54%, ≥55%, ≥56%, ≥57%, ≥58%, ≥59%, ≥60%, ≥61%, ≥62%, ≥63%, ≥64%, ≥65%, or ≥66% with propylene selectivity of ≥75%, ≥80%, ≥85%, ≥90%, ≥93%, or ≥95%. In some embodiments, when the hydrocarbon-containing feed contains propane and the upgraded hydrocarbon contains propylene, contact between the hydrocarbon-containing feed and the catalyst can result in a propylene yield of at least 48%, at least 49%, at least 50%, at least 51%, at least 52%, at least 53%, at least 55%, at least 57%, at least 60%, at least 62%, at least 63%, at least 64%, at least 65%, or at least 66% with a propylene selectivity of at least 75%, at least 80%, at least 30, at least 40, at least 50, at least 60, at least 60%, at least 60%, at least 60%, at least 60%, at least 60%, at least 60%, at least 60%, at least 64%, at least 65%, or at least 66% over at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 60%,In another embodiment, when a hydrocarbon-containing feed contains at least 70 vol%, at least 75 vol%, at least 80 vol%, at least 85 vol%, at least 90 vol%, or at least 95 vol% of propane based on the total volume of the hydrocarbon-containing feed, and is contacted under a propane partial pressure of at least 20 kPa absolute pressure, a propylene yield of at least 48%, at least 49%, at least 50%, at least 51%, at least 52%, at least 53%, at least 55%, at least 57%, at least 60%, at least 62%, at least 63%, at least 64%, at least 65%, or at least 66% can be obtained with a propylene selectivity of at least 75%, at least 80%, at least 85%, at least 90%, or at least 95% over at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 100 cycles, at least 125 cycles, at least 150 cycles, at least 175 cycles, or at least 200 cycles. It is believed that the propylene yield can be increased to at least 67%, at least 68%, at least 70%, at least 72%, at least 75%, at least 77%, at least 80%, at least 80%, at least 80%, or at least 82% with a propylene selectivity of at least 75%, at least 80%, at least 85%, at least 90%, or at least 95% over at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 100, at least 125, at least 150, at least 175, or at least 200 cycles, with a propylene selectivity of at least 67%, at least 68%, at least 70%, at least 72%, at least 75%, at least 77%, at least 80%, or at least 82%, with a propylene selectivity of at least 95%, at least 80%, at least 85%, at least 90%, or at least 82%, over at least 15, at least 20, at least 30, at least 40, at least 50, at least 60, at least 70, at least 100, at least 125, at least 150, at least 175, or at least 200 cycles.In some embodiments, this propylene yield can be obtained when the catalyst is contacted with a hydrocarbon feed at a temperature of at least 620°C, at least 630°C, at least 640°C, at least 650°C, at least 655°C, at least 660°C, at least 670°C, at least 680°C, at least 690°C, at least 700°C, or at least 750°C over at least 15, at least 200 cycles, at least 30, at least 40, at least 50, at least 60, at least 70, at least 100 cycles, at least 125 cycles, at least 150 cycles, at least 175 cycles, or at least 200 cycles.

[0027] Systems suitable for carrying out the processes disclosed herein include technically well-known systems, such as the fixed-bed reactor disclosed in International Publication No. WO2017078894; U.S. Patent Nos. 3,888,762, 7,102,050, 7,195,741, 7,122,160, and 8,653,317; and the fluid riser reactor and / or downer reactor disclosed in U.S. Patent Application Publication Nos. 2004 / 0082824 and 2008 / 0194891; and the reverse-flow reactor disclosed in U.S. Patent No. 8,754,276, U.S. Patent Application Publication No. 2015 / 0065767; and International Publication No. WO2013169461.

[0028] catalyst The catalyst contains Group 10 elements arranged on an inorganic support in amounts of 0.001 wt%, 0.002 wt%, 0.003 wt%, 0.004 wt%, 0.005 wt%, 0.006 wt%, 0.007 wt%, 0.008 wt%, 0.009 wt%, 0.01 wt%, 0.015 wt%, 0.02 wt%, 0.025 wt%, 0.03 wt%, 0.035 wt%, 0.04 wt%, 0.045 wt%, and 0.05 wt% based on the mass of the inorganic support. It may include wt%, 0.055wt%, 0.06wt%, 0.065wt%, 0.07wt%, 0.075wt%, 0.08wt%, 0.085wt%, 0.09wt%, 0.095wt%, 0.1wt%, 0.2wt%, 0.3wt%, 0.4wt%, 0.5wt%, 0.6wt%, 0.7wt%, 0.8wt%, 0.9wt%, or amounts from 1wt% to 2wt%, 3wt%, 4wt%, 5wt%, or 6wt%. In some embodiments, the catalyst composition is based on the mass of the inorganic support and is limited to ≤5.5wt%, ≤4.5wt%, ≤3.5wt%, ≤2.5wt%, ≤1.5wt%, ≤1wt%, ≤0.9wt%, ≤0.8wt%, ≤0.7wt%, ≤0.6wt%, ≤0.5wt%, ≤0.4wt%, ≤0.3wt%, ≤0.2wt%, ≤0.15wt%, ≤0.1wt%, ≤0.09wt%, and ≤0.08wt%. It may contain Group 10 elements disposed on an inorganic carrier in amounts of ≤0.07wt%, ≤0.06wt%, ≤0.05wt%, ≤0.04wt%, ≤0.03wt%, ≤0.02wt%, ≤0.01wt%, ≤0.009wt%, ≤0.008wt%, ≤0.007wt%, ≤0.006wt%, ≤0.005wt%, ≤0.004wt%, ≤0.003wt%, or ≤0.002wt%. In some embodiments, the catalyst may include, based on the mass of the inorganic support, >0.001, >0.003 wt%, >0.005 wt%, >0.007, >0.009 wt%, >0.01 wt%, >0.02 wt%, >0.04 wt%, >0.06 wt%, >0.08 wt%, >0.1 wt%, >0.13 wt%, >0.15 wt%, >0.17 wt%, >0.2 wt%, >0.23, >0.25 wt%, >0.27 wt%, or >0.3 wt% and <0.5 wt%, <1 wt%, <2 wt%, <3 wt%, <4 wt%, <5 wt%, or <6 wt% of Group 10 elements disposed on the inorganic support.In some embodiments, the Group 10 elements may be Ni, Pd, Pt, a combination thereof, or a mixture thereof. In at least one embodiment, the Group 10 elements may be Pt or contain Pt. When two or more Group 10 elements are arranged on an inorganic support, the catalyst is expressed in quantities of 0.001 wt%, 0.002 wt%, 0.003 wt%, 0.004 wt%, 0.005 wt%, 0.006 wt%, 0.007 wt%, 0.008 wt%, 0.009 wt%, 0.01 wt%, 0.015 wt%, 0.02 wt%, 0.025 wt%, 0.03 wt%, 0.035 wt%, 0.04 wt%, 0.045 wt%, 0.05 wt%, and 0.055 wt based on the mass of the inorganic support. It may include the total amount of two or more Group 10 elements disposed on an inorganic carrier, ranging from %, 0.06 wt%, 0.065 wt%, 0.07 wt%, 0.075 wt%, 0.08 wt%, 0.085 wt%, 0.09 wt%, 0.095 wt%, 0.1 wt%, 0.2 wt%, 0.3 wt%, 0.4 wt%, 0.5 wt%, 0.6 wt%, 0.7 wt%, 0.8 wt%, 0.9 wt%, or from 1 wt% to 2 wt%, 3 wt%, 4 wt%, 5 wt%, or 6 wt%. In some embodiments, one or more C2-C elements may be included. 16 Straight-chain or branched alkanes, or one or more C4-C 16 Cyclic alkanes, one or more C8-C 16 The active components of a regenerative catalyst, which may have the ability to cause one or more dehydrogenation, dehydrogenated aromatication, and dehydrogenated cyclization of a hydrocarbon-containing feed containing alkyl aromatic hydrocarbons or mixtures thereof, may contain Group 10 elements.

[0029] The inorganic support may be, but not limited to, one or more Group 2 elements, combinations thereof, or mixtures thereof. In some embodiments, the Group 2 elements may exist in elemental form. In other embodiments, the Group 2 elements may exist in compound form. For example, the Group 2 elements may exist as oxides, phosphates, halides, halates, sulfates, sulfides, borates, nitrides, carbides, aluminates, aluminosilicates, silicates, carbonates, metaphosphates, selenides, tungstates, molybdates, chromates, chromates, dichromates, or silide. In some embodiments, mixtures of any two or more compounds containing Group 2 elements may exist in various forms. For example, the first compound may be an oxide and the second compound may be an aluminate. In this case, the first and second compounds may contain the same or different Group 2 elements.

[0030] Inorganic carriers are classified based on their mass as follows: ≥0.5wt%, ≥1wt%, ≥2wt%, ≥3wt%, ≥4wt%, ≥5wt%, ≥6wt%, ≥7wt%, ≥8wt%, ≥9wt%, ≥10wt%, ≥11wt%, ≥12wt%, ≥13wt%, ≥14wt%, ≥15wt%, ≥16wt%, ≥17wt%, ≥18wt%, ≥19wt%, ≥20wt%, ≥21wt% It may contain Group 2 elements in the following proportions: ≥22 wt%, ≥23 wt%, ≥24 wt%, ≥25 wt%, ≥26 wt%, ≥27 wt%, ≥28 wt%, ≥29 wt%, ≥30 wt%, ≥35 wt%, ≥40 wt%, ≥45 wt%, ≥50 wt%, ≥55 wt%, ≥60 wt%, ≥65 wt%, ≥70 wt%, ≥75 wt%, ≥80 wt%, ≥85 wt%, or ≥90 wt%. In some embodiments, the inorganic carrier may contain Group 2 elements ranging from 0.5 wt%, 1 wt%, 2 wt%, 2.5 wt%, 3 wt%, 5 wt%, 7 wt%, 10 wt%, 11 wt%, 13 wt%, 15 wt%, 17 wt%, 19 wt%, 21 wt%, 23 wt%, or 25 wt% to 30 wt%, 35 wt%, 40 wt%, 45 wt%, 50 wt%, 55 wt%, 60 wt%, 65 wt%, 70 wt%, 75 wt%, 80 wt%, 85 wt%, 90 wt%, or 92.34 wt%, based on the mass of the inorganic carrier. In some embodiments, the molar ratio of Group 2 elements to Group 10 elements is 0.24, 0.5, 1, 10, 50, 100, 300, 450, 600, 800, 1,000, 1,200, 1,500, 1,700, or 2,000 to 3,000, 3,500, 4,000, 4,500, 5,000, 5,500, 6,000, 6,500, 7,000, 7,500, 8,000, 8,500, 9,000, 9,500, 10,000, 15,000. It may be in the range of 20,000, 25,000, 30,000, 35,000, 40,000, 45,000, 50,000, 55,000, 60,000, 65,000, 70,000, 75,000, 80,000, 85,000, 90,000, 95,000, 100,000, 200,000, 300,000, 400,000, 500,000, 600,000, 700,000, 800,000, or up to 900,000.

[0031] In some embodiments, the inorganic support may contain a group 2 element and Al, and may be in the form of a mixed group 2 element / Al metal oxide having O, Mg, and Al atoms mixed on an atomic scale. In some embodiments, the inorganic support may be a group 2 element in the form of an oxide that can be mixed on an nm scale and Al or one or more oxides of group 2 elements and Al2O3, or may include these. In some embodiments, the inorganic support may be an oxide of a group 2 element mixed on an nm scale, for example, MgO and Al2O3, or may include these. In some embodiments, the inorganic support may be a first amount of a group 2 element and Al in the form of a mixed group 2 element / Al metal oxide, and a second amount of a group 2 element in the form of an oxide of a group 2 element, or may contain these. In these embodiments, the mixed group 2 element / Al metal oxide and the oxide of a group 2 element may be mixed on an nm scale, and the group 2 element and Al in the mixed group 2 element / Al metal oxide may be mixed on an atomic scale. In other embodiments, the inorganic support may be a first amount of a group 2 element and a first amount of Al in the form of a mixed group 2 element / Al metal oxide, a second amount of a group 2 element in the form of an oxide of a group 2 element, and a second amount of Al in the form of Al2O3, or contain these. In these embodiments, the mixed group 2 element / Al metal oxide, the oxide of a group 2 element, and Al2O3 may be mixed on an nm scale, and the group 2 element and Al in the mixed group 2 element / Al metal oxide may be mixed on an atomic scale.

[0032] In some embodiments, when the inorganic support contains a group 2 element and Al, the mass ratio of the group 2 element to Al in the inorganic support may be in the range of 0.001, 0.005, 0.01, 0.05, 0.1, 0.15, 0.2, 0.3, 0.5, 0.7, or 1 to 3, 6, 12.5, 25, 50, 75, 100, 200, 300, 400, 500, 600, 700, 800, 900, or 1,000. In some embodiments, when the inorganic carrier contains Al, the inorganic carrier may contain Al in amounts ranging from 0.5 wt%, 1 wt%, 1.5 wt%, 2 wt%, 2.1 wt%, 2.3 wt%, 2.5 wt%, 2.7 wt%, 3 wt%, 4 wt%, 5 wt%, 6 wt%, 7 wt%, 8 wt%, 9 wt%, 10 wt%, or 11 wt% to 15 wt%, 20 wt%, 25 wt%, 30 wt%, 40 wt%, 45 wt%, or 50 wt%, based on the mass of the inorganic carrier. In some embodiments, the inorganic support may be one or more of the following compounds, or may include them: Mg w Al2O 3+w (w is a positive number); Ca x Al2O 3+x (x is a positive number); Sr y Al2O 3+y (y is a positive number); Ba z Al2O 3+z (z is a positive number); BeO; MgO; CaO; BaO; SrO; BeCO3; MgCO3; CaCO3; SrCO3, BaCO3; CaZrO3; Ca7ZrAl6O 18 CaTiO3;Ca7Al6O 18 Ca7HfAl6O 18;BaCeO3; one or more magnesium chromates, one or more magnesium tungstates, one or more magnesium molybdates, combinations thereof, and mixtures thereof. In some embodiments, the group 2 elements may include Mg, and at least a portion of the group 2 elements may be in the form of MgO or a mixed oxide containing MgO. In some embodiments, the inorganic support may be, but not limited to, a MgO-Al2O3 mixed metal oxide or contain the same. In some embodiments, when the inorganic support is a MgO-Al2O3 mixed metal oxide, the inorganic support may have a molar ratio of Mg to Al equal to 20, 10, 5, 2, 1 to 0.5, 0.1, or 0.01.

[0033] Mg w Al2O 3+w (where w is a positive number) may have a molar ratio of Mg to Al ranging from 0.5, 1, 2, 3, 4, or 5 to 6, 7, 8, 9, or 10 when present as an inorganic support or as a component of an inorganic support. In some embodiments, Mg w Al2O 3+w This may include MgAl2O4, Mg2Al2O5, or a mixture thereof. Ca x Al2O 3+x (where x is a positive number) may have a molar ratio of Ca to Al in the range of 1:12, 1:4, 1:2, 2:3, 5:6, 1:1, 12:14, or 1.5:1 when present as an inorganic carrier or as a component of an inorganic carrier. In some embodiments, Ca x Al2O 3+x This may include tricalcium aluminate, dodecalcium heptaluminate, monocalcium aluminate, monocalcium dialuminate, monocalcium hexaluminate, dicalcium aluminate, pentacalcium trialuminate, tetracalcium trialuminate, or any mixture thereof. Sr y Al2O 3+y (where y is a positive number) may have a molar ratio of Sr to Al ranging from 0.05, 0.3, or 0.6 to 0.9, 1.5, or 3 when present as an inorganic support or as a component of an inorganic support. z Al2O 3+z(where z is a positive number) may have a molar ratio of Ba to Al ranging from 0.05, 0.3, or 0.6 to 0.9, 1.5, or 3 when present as an inorganic support or as a component of an inorganic support.

[0034] In some embodiments, the inorganic support may also include one or more accelerators disposed thereon. The accelerators may be, but are not limited to, Sn, Ag, Cu, combinations thereof, or mixtures thereof. In some embodiments, the accelerator may be associated with a Group 10 element, such as Pt. For example, an accelerator and a Group 10 element disposed on the inorganic support may form a Group 10 element-accelerator cluster that can be dispersed on the inorganic support. If present, the accelerator can improve the selectivity / activity / lifetime of the catalyst for a given upgraded hydrocarbon. In some embodiments, the addition of an accelerator can improve the propylene selectivity of the catalyst when the hydrocarbon-containing feed contains propane. The catalyst may contain an accelerator in amounts ranging from 0.01 wt%, 0.1 wt%, 0.2 wt%, 0.3 wt%, 0.4 wt%, 0.5 wt%, 0.6 wt%, 0.7 wt%, 0.8 wt%, 0.9 wt%, or from 1 wt% to 3 wt%, 5 wt%, 7 wt%, or 10 wt%, based on the mass of the inorganic support.

[0035] In some embodiments, the inorganic support may also include one or more alkali metal elements disposed thereon. The alkali metal elements, if present, may be, but not limited to, Li, Na, K, Rb, Cs, combinations thereof, or mixtures thereof. In at least some embodiments, the alkali metal elements may be K and / or Cs, or include them. If present, the alkali metal elements can improve the selectivity of the catalyst for a given upgraded hydrocarbon. The catalyst may contain alkali metal elements in amounts ranging from 0.01 wt%, 0.1 wt%, 0.2 wt%, 0.3 wt%, 0.4 wt%, 0.5 wt%, 0.6 wt%, 0.7 wt%, 0.8 wt%, 0.9 wt%, or from 1 wt% to 2 wt%, 3 wt%, 4 wt%, or 5 wt%, based on the mass of the inorganic support. In some embodiments, suitable catalysts include those described in U.S. Patent Nos. 5,073,662 and 6,313,063; U.S. Patent Publication Nos. 2011 / 0301392 and 2005 / 0003960; and European Patent Publication Nos. EP0486993A1 and EP1073516A1.

[0036] In some embodiments, the inorganic support may also include, but is not limited to, at least one metallic element and / or at least one metalloid element selected from groups other than Group 2 and Group 10, and / or at least one compound thereof, in which case the at least one metallic element and / or at least one metalloid element is not Li, Na, K, Rb, Cs, Sn, Ag, or Cu. If the support also includes a compound containing a metallic element and / or metalloid element selected from groups other than Group 2 and Group 10, the at least one metallic element and / or at least one metalloid element is not Li, Na, K, Rb, Cs, Sn, Ag, or Cu, and the compound may exist in the support as an oxide, phosphate, halide, halate, sulfate, sulfide, borate, nitride, carbide, aluminate, aluminosilicate, silicate, carbonate, metaphosphate, selenide, tungstate, molybdate, chromate, chromate, dichromate, or silicide. In some embodiments, suitable compounds include metallic elements and / or metalloid elements selected from groups other than Group 2 and Group 10, wherein at least one metallic element and / or at least one metalloid element is not Li, Na, K, Rb, Cs, Sn, Ag, or Cu, but are not limited to the following: B2O3, AlBO3, Al2O3, SiO2, SiC, Si3N4, aluminosilicate, zinc aluminate, ZnO, VO, V2O3, VO2, V2O5, Ga s O t In u O v Mn2O3, Mn3O4, MnO, one or more molybdenum oxides, one or more tungsten oxides, one or more zeolites (where s, t, u, and v are positive numbers), and mixtures and combinations thereof, or may contain thereof.

[0037] The preparation of inorganic supports can be achieved by any known process. For simplicity and ease of explanation, the preparation of suitable inorganic supports containing mixed magnesium and aluminum oxides (Mg(Al)O or MgO / Al2O3) will be described in more detail. Catalyst synthesis techniques are well known, and the following description is for illustrative purposes only and should not be considered limiting to the synthesis of inorganic supports or catalysts. In some embodiments, to produce a MgO / Al2O3 mixed oxide inorganic support, precursors of Mg and Al, such as Mg(NO3)2 and Al(NO3)3, may be mixed together, for example, ball-milled and then calcined. In another embodiment, the two precursors may be dissolved in H2O, stirred until dry (sometimes with heat), and then calcined to produce an inorganic support. In yet another embodiment, the two precursors may be dissolved in H2O, after which a base and a carbonate, such as NaOH / Na2CO3, may be added to produce hydrotalcite and then calcined to produce an inorganic support. In another embodiment, commercially available ready-made MgO and Al2O3 may be mixed and ball-milled to produce an inorganic support. In another embodiment, a Mg(NO3)2 precursor may be dissolved in H2O, and this solution may be impregnated onto an existing inorganic support, such as an Al2O3 inorganic support, which may then be dried and calcined to produce an inorganic support. In yet another embodiment, Mg from Mg(NO3)2 may be loaded onto an existing Al2O3 inorganic support via ion adsorption, followed by liquid-solid separation, drying and calcination to produce an inorganic support. While we do not wish to be bound by theory, the inorganic supports produced by any of the above methods and / or other methods may include (i) Mg and Al mixed together on an nm scale, (ii) Mg and Al in the form of a mixed Mg / Al metal oxide, or (iii) a combination of (i) and (ii).

[0038] Group 10 metals and any accelerators and / or alkali metal elements can be loaded onto a mixed oxide inorganic support by any known technique. For example, one or more Group 10 element precursors, e.g., chloroplatinic acid, tetraammineplatinate nitrate, and / or tetraammineplatinate hydroxide, one or more accelerator precursors (if used), e.g., salts of SnCl4 and / or AgNO3, and one or more alkali metal element precursors (if used), e.g., KNO3, KCl, and / or NaCl, can be dissolved in water. This solution can be impregnated onto an inorganic support and then dried and calcined. In some embodiments, the Group 10 element precursors and optionally the accelerator precursors and / or alkali metal element precursors can be loaded onto the inorganic support simultaneously or separately in a sequence separated by drying and / or calcination steps. In other embodiments, Group 10 elements and optionally accelerators and / or alkali metal elements may be deposited onto an inorganic support by chemical vapor deposition, in which case the precursors are volatilized and deposited onto the support before being calcined. In other embodiments, Group 10 element precursors and optionally accelerator precursors and / or alkali metal precursors may be deposited onto an inorganic support via ion adsorption, followed by liquid-solid separation, drying and calcination. Optionally, the catalyst may be synthesized using a one-pot synthesis method, in which the inorganic support precursors, Group 10 metal active phase and accelerator are all mixed together dry or wet, with or without any other additives to aid the synthesis, followed by drying and calcination.

[0039] Suitable processes that can be used for preparing the catalysts disclosed herein include those described in U.S. Patent Nos. 4,788,371; 4,962,265; 5,922,925; 8,653,317; European Patent No. EP0098622; Journal of Catalysis 94 (1985), pp. 547-557; and / or Applied Catalysis 54 (1989), pp. 79-90. When examined under a scanning electron microscope or transmission electron microscope, the as-synthesized catalyst may appear as primary particles, aggregates of primary particles, aggregated primary particles, or combinations thereof. When examined under a scanning electron microscope or transmission electron microscope, the primary particles in the as-synthesized catalyst may have an average particle size ranging from 0.2 nm, 0.5 nm, 1 nm, 5 nm, 10 nm, 25 nm, 30 nm, 40 nm, 50 nm, 60 nm, 70 nm, 80 nm, 90 nm, 100 nm, 150 nm, 200 nm, 250 nm, 300 nm, 350 nm, 400 nm, 450 nm, or 500 nm to 1 μm, 10 μm, 25 μm, 50 μm, 100 μm, 150 μm, 200 μm, 250 μm, 300 μm, 400 μm, or 500 μm, for example, a diameter in the case of a sphere. In some embodiments, the catalyst particles may have an average cross-sectional length of 0.2 nm to 500 μm, 0.5 nm to 300 μm, 1 nm to 200 μm, 2 nm to 100 μm, or 2 nm to 500 μm as measured by a transmission electron microscope. The catalyst is 0.1m 2 / g, 1m 2 / g, 10m 2 / g, or 100m 2 / g to 500m 2 / g, 800m 2 / g, 1,000m 2 / g, or 1,500m 2 The catalyst may have a surface area ranging from 1 / g. The catalyst surface area can be measured according to the Brunauer-Emmett-Teller (BET) method, which utilizes nitrogen adsorption-desorption (at liquid nitrogen temperature, 77K) using a Micromeritics 3flex instrument after degassing the powder at 350°C for 4 hours. Further information on this method can be found, for example, in “Characterization of Porous Solids and Powders: Surface Area, Pore Size and Density,” S. Lowell et al., Springer, 2004.

[0040] In some embodiments, the inorganic carrier may be formed by extrusion or by other means into any desired monolithic structure on which Group 10 elements and any optional accelerators and / or alkali metal elements may be arranged. Suitable monolithic structures may be, but are not limited to, structures having multiple substantially parallel internal passages, such as structures in the form of ceramic honeycomb. In some embodiments, the carrier may be in the form of beads, spheres, rings, donut shapes, irregular shapes, rods, cylinders, flakes, films, cubes, polygonal shapes, sheets, fibers, coils, helices, meshes, sintered porous masses, granules, pellets, tablets, powders, fine particles, extruded materials, cloth or web-type materials, or honeycomb matrix monoliths (including crushed or broken forms) on which Group 10 elements and any optional accelerators and / or alkali metal elements may be arranged. The as-synthesized catalyst can be formulated into one or more forms suitable for various short-cycle (≤5 hours) hydrocarbon upgrade processes. Alternatively, the support can be formulated into a form suitable for various short-cycle hydrocarbon upgrade processes before the addition of Group 10 elements and any optional accelerators and / or alkali metal elements. During formulation, one or more binders and / or additives can be added to the catalyst and / or support to improve the chemical / physical properties of the catalyst. For example, spray-dried catalyst particles with an average cross-sectional diameter typically ranging from 40 μm to 100 μm are used in FCC-type fluidized bed reactors. To prepare a spray-dried catalyst, it is necessary to slurry the support / catalyst with a binder / additive before spray-drying and calcination, so that the binder / additive is present in the slurry.

[0041] Hydrocarbon Upgrade Process Returning to the hydrocarbon upgrade process, the hydrocarbon-containing feed and at least a portion of the catalyst and / or regenerated catalyst can be brought into contact with each other in any suitable environment, for example, in one or more reaction zones or conversion zones located in one or more reactors, to produce effluent and at least partially deactivated catalyst. In some embodiments, the reaction zones or conversion zones may be located in or otherwise within one or more fixed-bed reactors, one or more fluid or moving-bed reactors, one or more back-flow reactors, or any combination thereof. The hydrocarbon-containing feed and at least a portion of the catalyst and / or regenerated catalyst may be in contact at temperatures ranging from 300°C, 350°C, 400°C, 450°C, 500°C, 550°C, 600°C, 620°C, 650°C, 660°C, 670°C, 680°C, 690°C, or from 700°C to 725°C, 750°C, 760°C, 780°C, 800°C, 825°C, 850°C, 875°C, or 900°C. In some embodiments, the hydrocarbon-containing feed and at least a portion of the catalyst and / or regenerated catalyst may be in contact at temperatures ranging from at least 620°C, at least 650°C, at least 660°C, at least 670°C, at least 680°C, at least 690°C, or from at least 700°C to 725°C, 750°C, 760°C, 780°C, 800°C, 825°C, 850°C, 875°C, or 900°C. The hydrocarbon-containing feed is introduced into a reaction zone or conversion zone, where it may be in contact with at least a portion of the catalyst and / or regenerated catalyst for a period of time of ≤3 hours, ≤2.5 hours, ≤2 hours, ≤1.5 hours, ≤1 hour, ≤45 minutes, ≤30 minutes, ≤20 minutes, ≤10 minutes, ≤5 minutes, ≤1 minute, ≤30 seconds, ≤10 seconds, ≤5 seconds, or ≤1 second or ≤0.5 seconds. In some embodiments, the hydrocarbon-containing feed may be in contact with at least a portion of the catalyst and / or regenerating catalyst for a period of time ranging from 0.1 seconds, 0.5 seconds, 0.7 seconds, 1 second, 30 seconds, 1 minute, 5 minutes, or 10 minutes to 30 minutes, 50 minutes, 70 minutes, 1.5 hours, 2 hours, or 3 hours.

[0042] At least a portion of the hydrocarbon-containing feed and the catalyst and / or regenerated catalyst may be brought into contact under a hydrocarbon partial pressure of at least 20 kPa absolute pressure, in which case the hydrocarbon partial pressure is such that any C2-C in the hydrocarbon-containing feed 16 Alkane and both C8-C 16 This is the total partial pressure of alkyl aromatic hydrocarbons. In some embodiments, the partial pressure of hydrocarbons during contact between the hydrocarbon-containing feed and at least a portion of the catalyst and / or regenerating catalyst may range from 20 kPa absolute pressure, 50 kPa absolute pressure, 100 kPa absolute pressure, at least 150 kPa, at least 200 kPa absolute pressure, 300 kPa absolute pressure, 500 kPa absolute pressure, 750 kPa absolute pressure, or from 1,000 kPa absolute pressure to 1,500 kPa absolute pressure, 2,500 kPa absolute pressure, 4,000 kPa absolute pressure, 5,000 kPa absolute pressure, 7,000 kPa absolute pressure, 8,500 kPa absolute pressure, or 10,000 kPa absolute pressure, in which case the partial pressure of hydrocarbons is the total partial pressure of any C2-C in the hydrocarbon-containing feed. 16 Alkane and both C8-C 16 This is the total partial pressure of alkyl aromatic hydrocarbons. In other embodiments, the partial pressure of hydrocarbons in contact with at least a portion of the hydrocarbon-containing feed and the catalyst and / or regenerating catalyst may range from 20 kPa absolute pressure, 50 kPa absolute pressure, 100 kPa absolute pressure, 150 kPa absolute pressure, 200 kPa absolute pressure, 250 kPa absolute pressure, or 300 kPa absolute pressure to 500 kPa absolute pressure, 600 kPa absolute pressure, 700 kPa absolute pressure, 800 kPa absolute pressure, 900 kPa absolute pressure, or 1,000 kPa absolute pressure, in which case the partial pressure of hydrocarbons is the total partial pressure of any C2-C in the hydrocarbon-containing feed. 16 Alkane and both C8-C 16 This is the total partial pressure of alkyl aromatic hydrocarbons.

[0043] In some embodiments, the hydrocarbon-containing feed is composed of at least 60 vol%, at least 65 vol%, at least 70 vol%, at least 75 vol%, at least 80 vol%, at least 85 vol%, at least 90 vol%, at least 95 vol%, or at least 99 vol% single C2-C based on the total volume of the hydrocarbon-containing feed. 16Alkanes, such as propane, may be included. At least a portion of the hydrocarbon-containing feed and catalyst and / or regenerating catalyst may contain a single C2-C at an absolute pressure of at least 20 kPa, at least 50 kPa, at least 100 kPa, at least 150 kPa, at least 250 kPa, at least 300 kPa, at least 400 kPa, at least 500 kPa, or at least 1,000 kPa. 16 Alkanes, for example, can be contacted under pressure with propane. The hydrocarbon-containing feed can be brought into contact with at least a portion of the catalyst and / or regenerating catalyst within the reaction zone or conversion zone at any mass per hour space velocity (WHSV) effective for carrying out the upgrade process. In some embodiments, the WHSV is 0.01 hours. -1 , 0.1 hours -1 , 1 hour -1 , 2 hours -1 , 5 hours -1 , 10 hours -1 , 20 hours -1 , 30 hours -1 , or 50 hours -1 From 100 hours -1 , 250 hours -1 , 500 hours -1 , or 1,000 hours -1 It may be up to. In some embodiments, when the hydrocarbon upgrade process includes a catalyst that is fluidized or otherwise moved and / or a moving regenerating catalyst, the circulating mass flow rate of the catalyst is C2-C 16 Alkane and both C8-C 16 The ratio of the mass flow rate of alkyl aromatic hydrocarbons to the total amount may be within the range of 1, 3, 5, 10, 15, 20, 25, 30, or 40 on a mass-to-mass basis, up to 50, 60, 70, 80, 90, 100, 110, 125, or 150.

[0044] When the activity of at least partially deactivated catalyst decreases to below a desired minimum amount, at least partially deactivated catalyst or at least a portion thereof can undergo the regeneration process described above to produce a regenerated catalyst. Regeneration of at least partially deactivated catalyst can occur in the reaction zone or conversion zone, or in a separate combustion zone separate from the reaction zone or conversion zone, depending on the specific reactor configuration, to produce a regenerated catalyst. For example, catalyst regeneration can occur in the reaction zone or conversion zone when a fixed-bed reactor or backflow reactor is used, or in a separate combustion zone, which may be another separate combustion zone, when a fluidized-bed reactor or other circulating or fluidized-type reactor is used. Similarly, an optional reduction step may occur in the reaction zone or conversion zone, in the combustion zone, and / or in a separate reduction zone. Therefore, in circulating processes such as those commonly used in fixed-bed reactors and back-flow reactors, and / or continuous processes commonly used in fluidized-bed reactors, the hydrocarbon-containing feed can be brought into contact with a catalyst to cause one or more of the hydrocarbon-containing feed to undergo dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization, thereby producing a coking catalyst and a first effluent containing one or more upgraded hydrocarbons and molecular hydrogen. If necessary, one or more separators, such as cyclone separators, can be used to separate the effluent containing the upgraded hydrocarbons and molecular hydrogen from the coking catalyst. As described above, the oxidizing gas may be, but not limited to, O2, O3, CO2, or a mixture thereof, and may contain 5 mol% or less of H2O. In some embodiments, an amount of oxidizing gas exceeding the amount required for 100% combustion of the contaminants placed on the catalyst, such as coke, can be used to increase the rate of contaminant removal from the catalyst, thereby reducing the time required for contaminant removal and resulting in an increased yield of the upgraded product produced within a given time.

[0045] Hydrocarbon-containing feed C2-C 16Alkanes are, but are not limited to, ethane, propane, n-butane, isobutane, n-pentane, isopentane, n-hexane, 2-methylpentane, 3-methylpentane, 2,2-dimethylbutane, n-heptane, 2-methylhexane, 2,2,3-trimethylbutane, cyclopentane, cyclohexane, methylcyclopentane, ethylcyclopentane, n-propylcyclopentane, 1,3-dimethylcyclohexane, or mixtures thereof, or may include these. For example, a hydrocarbon-containing feed may include propane, which can be dehydrogenated to produce propylene, and / or isobutane, which can be dehydrogenated to produce isobutylene. In another example, a hydrocarbon-containing feed may include liquefied petroleum gas (LPG), which may be in the gas phase upon contact with the catalyst. In some embodiments, the hydrocarbons in the hydrocarbon-containing feed may consist substantially of a single alkane, such as propane. In some embodiments, the hydrocarbon-containing feed is a single C2-C mixture of ≥50 mol%, ≥75 mol%, ≥95 mol%, ≥98 mol%, or ≥99 mol%, based on the total mass of all hydrocarbons in the hydrocarbon-containing feed. 16 Alkanes, such as propane, may be included. In some embodiments, the hydrocarbon-containing feed is composed of at least 50 vol%, at least 55 vol%, at least 60 vol%, at least 65 vol%, at least 70 vol%, at least 75 vol%, at least 80 vol%, at least 85 vol%, at least 90 vol%, at least 95 vol%, at least 97 vol%, or at least 99 vol% single C2-C based on the total volume of the hydrocarbon-containing feed. 16 This may include alkanes, such as propane.

[0046] C8-C 16 Alkyl aromatic hydrocarbons are, but are not limited to, ethylbenzene, propylbenzene, butylbenzene, one or more ethyltoluenes, or mixtures thereof, or may include these. In some embodiments, the hydrocarbon-containing feed is a single C8-C hydrocarbon in a total mass of ≥50 mol%, ≥75 mol%, ≥95 mol%, ≥98 mol%, or ≥99 mol%, based on the total mass of all hydrocarbons in the hydrocarbon-containing feed. 16Alkyl aromatic hydrocarbons, such as ethylbenzene, may be included. In some embodiments, ethylbenzene can be dehydrogenated to produce styrene. Therefore, in some embodiments, the processes disclosed herein may include propane dehydrogenation, butane dehydrogenation, isobutane dehydrogenation, pentane dehydrogenation, pentane dehydrogenation cyclization to cyclopentadiene, naphtha modification, ethylbenzene dehydrogenation, ethyltoluene dehydrogenation, and the like.

[0047] In some embodiments, the hydrocarbon-containing feed may be diluted with one or more diluents, such as one or more inert gases. Suitable inert gases are, but are not limited to, Ar, Ne, He, N2, CO2, CH4, or mixtures thereof, or may include these. If the hydrocarbon-containing feed contains diluents, the hydrocarbon-containing feed contains any C2-C 16 Alkane and both C8-C 16 The diluent may be present in amounts ranging from 0.1 vol%, 0.5 vol%, 1 vol%, or 2 vol%, to 3 vol%, 8 vol%, 16 vol%, or 32 vol%, based on the total volume of alkyl aromatic hydrocarbons. In some embodiments, the hydrocarbon-containing feed may also contain H2. In some embodiments, when the hydrocarbon-containing feed contains H2, H2 and any C2-C 16 Alkane and both C8-C 16 The molar ratio of the total amount of alkyl aromatic hydrocarbons may be 0.1, 0.3, 0.5, 0.7, or within the range of 1 to 2, 3, 4, 5, 6, 7, 8, 9, or 10.

[0048] In some embodiments, the hydrocarbon-containing feed contains virtually no water vapor, for example, any C2-C in the hydrocarbon-containing feed. 16 Alkane and both C8-C 16 Based on the total volume of alkyl aromatic compounds, there may be <0.1 vol% water vapor. In other embodiments, the hydrocarbon-containing feed may contain water vapor. For example, the hydrocarbon-containing feed may contain any C2-C in the hydrocarbon-containing feed. 16Alkanes and any C8-C 16 Based on the total volume of alkanes and any C8-C alkyl aromatic hydrocarbons, it may contain steam from 0.1 vol%, 0.3 vol%, 0.5 vol%, 0.7 vol%, 1 vol%, 3 vol%, or 5 vol% to 10 vol%, 15 vol%, 20 vol%, 25 vol%, 30 vol%, 35 vol%, 40 vol%, 45 vol%, or 50 vol%. In other embodiments, the hydrocarbon-containing feed is any C2-C in the hydrocarbon-containing feed 16 Alkanes and any C8-C 16 Based on the total volume of alkanes and any C8-C alkyl aromatic hydrocarbons, it may contain ≤ 50 vol%, ≤ 45 vol%, ≤ 40 vol%, ≤ 35 vol%, ≤ 30 vol%, ≤ 25 vol%, ≤ 20 vol%, or ≤ 15 vol% of steam. In other embodiments, the hydrocarbon-containing feed is any C2-C in the hydrocarbon-containing feed 16 Alkanes and any C8-C 16 Based on the total volume of alkanes and any C8-C alkyl aromatic hydrocarbons, it may contain at least 1 vol%, at least 3 vol%, at least 5 vol%, at least 10 vol%, at least 15 vol%, at least 20 vol%, at least 25 vol%, or at least 30 vol% of steam.

[0049] In some embodiments, the hydrocarbon-containing feed can contain sulfur. For example, the hydrocarbon-containing feed may contain sulfur in the range from 0.5 ppm, 1 ppm, 5 ppm, 10 ppm, 20 ppm, 30 ppm, 40 ppm, 50 ppm, 60 ppm, 70 ppm, or 80 ppm to 100 ppm, 150 ppm, 200 ppm, 300 ppm, 400 ppm, or 500 ppm. In other embodiments, the hydrocarbon-containing feed may contain sulfur in the range of 1 ppm to 10 ppm, 10 ppm to 20 ppm, 20 ppm to 50 ppm, 50 ppm to 100 ppm, or 100 ppm to 500 ppm. Sulfur, when present in the hydrocarbon-containing feed, although not limited to, can be H2S, dimethyldisulfide, one or more mercaptans, or any mixture thereof or include these. Hydrocarbon feeds may contain substantially no or no molecular oxygen. In some embodiments, the hydrocarbon feed may contain ≤5 mol%, ≤3 mol%, or ≤1 mol% molecular oxygen (O2). Supplying a hydrocarbon feed substantially free of molecular oxygen is thought to substantially prevent oxidative coupling reactions that would otherwise consume at least some of the alkanes and / or alkyl aromatic hydrocarbons in the hydrocarbon feed.

[0050] Upgraded hydrocarbon recovery and use The upgraded hydrocarbon may include at least one upgraded hydrocarbon, such as an olefin, water, unreacted hydrocarbon, molecular hydrogen, etc. The upgraded hydrocarbon can be recovered or obtained by other means via any convenient process, for example, by one or more conventional processes. One such process may include the step of cooling and / or compressing the effluent to concentrate at least a portion of any water and any heavy hydrocarbons present, leaving mainly the olefin and any unreacted alkane or alkyl aromatic hydrocarbon in the gas phase. The olefin and unreacted alkane or alkyl aromatic hydrocarbon can then be removed from the reaction product in one or more separator drums. For example, the dehydrogenated product can be separated from the unreacted hydrocarbon feed using one or more splitters or distillation columns. In some embodiments, recovered olefins, such as propylene, can be used to produce polymers. For example, recovered propylene can be polymerized to produce polymers having segments or units derived from recovered propylene, such as polypropylene, ethylene-propylene copolymer, etc. Recovered isobutene can be used to produce one or more oxygen-containing compounds, such as methyl tert-butyl ether, fuel additives, such as diisobutene, or synthetic elastomer polymers, such as butyl rubber. [Examples]

[0051] Examples: The above considerations can be further explained by referring to the following non-limiting examples. Catalysts 1-27 and comparative catalysts were prepared according to the following procedure. Catalyst 1: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG70 / 170 (Sasol), a mixed metal oxide of MgO-Al2O obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 70 wt% MgO and 30 wt% Al2O3. According to Sasol, the BET surface area was 170 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.103g) (Acros Organics), chloroplatinic acid hexahydrate (0.0184g) (BioXtra), and deionized water (2.2mL) in a small glass vial. This solution was impregnated into a PURALOX® MG70 / 170 support. The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn. Catalyst 2: The catalyst was prepared according to the following procedure. 3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.134g) (Acros Organics), chloroplatinic acid hexahydrate (0.024g) (BioXtra), and deionized water (2.25mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was left in a sealed container at room temperature for 24 hours, then dried in air at 110°C for 6 hours, and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn.

[0052] Catalyst 3: The catalyst was a Sn-containing Pt-based catalyst supported on a Mg / Al mixed oxide support. Elemental analysis showed that the catalyst contained 0.48 wt% Pt, 1.25 wt% Sn, 67.93 wt% Mg, and 29.23 wt% Al, based on the total mass of the metal elements, with a molar ratio of Mg to Al of approximately 2.58. Catalyst 4: The catalyst was prepared according to the following procedure. 3 g of PURALOX® MG30 / 260 (Sasol), a mixed metal oxide of MgO-Al2O obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 30 wt% MgO and 70 wt% Al2O3. According to Sasol, the BET surface area was 260 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.134g) (Acros Organics), chloroplatinic acid hexahydrate (0.024g) (BioXtra), and deionized water (3.15mL) in a small glass vial. This solution was impregnated into a PURALOX® MG30 / 260 support. The impregnated material was stored in a sealed container at room temperature for 120 hours, then dried in air at 110°C for 6 hours, and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn. Catalyst 5: The catalyst was prepared according to the following procedure. 3 g of PURALOX® MG30 / 70 (Sasol), a mixed metal oxide of MgO-Al2O obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 30 wt% MgO and 70 wt% Al2O3. According to Sasol, the BET surface area was 70 m². 2 / g. Puralox MG30 / 70 contained more MgAl2O4 spinel phase than Puralox MG30 / 260. Tin(IV) chloride pentahydrate (0.134 g) (Acros Organics), chloroplatinic acid hexahydrate (0.024 g) (BioXtra), and deionized water (2.4 mL) were mixed in a small glass vial to make a solution. This solution was impregnated onto the PURALOX® MG30 / 70 support. The impregnated material was stored in a sealed container at room temperature for 120 hours, then dried in air at 110 °C for 6 hours and calcined at 800 °C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn.

[0053] Catalyst 6: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG28 / 100 (Sasol), which is mainly MgAl2O4 spinel, was secured. According to Sasol, the BET surface area was 100 m 2 / g. Tin(IV) chloride pentahydrate (0.103 g) (Acros Organics), chloroplatinic acid hexahydrate (0.0184 g) (BioXtra), and deionized water (2.4 mL) were mixed in a small glass vial to make a solution. This solution was impregnated onto the PURALOX® MG28 / 100 support. The impregnated material was dried in air at 110 °C for 6 hours and calcined at 800 °C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn. Catalyst 7: The catalyst was prepared according to the following procedure. 3.5 g of PURAL® MG70 (Sasol), a Mg / Al hydrotalcite, was secured. When activated at 550°C for 3 hours, it forms an MgO-Al2O3 mixed metal oxide containing 70 wt% MgO and 30 wt% Al2O3. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.103 g) (Acros Organics), chloroplatinic acid hexahydrate (0.0184 g) (BioXtra), and deionized water (2.6 mL) in a small glass vial. This solution was impregnated into a PURAL 70 support. The impregnated material was stored in a sealed container at room temperature for 24 hours, then dried in air at 110°C for 6 hours, and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn. Catalyst 8: The catalyst was prepared according to the following procedure. 2.5 g of MgO (50 nm, Sigma Aldrich) was secured. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.0158 g) (Acros Organics), chloroplatinic acid hexahydrate (0.0314 g) (BioXtra), and deionized water (1 mL) in a small glass vial. This solution was impregnated into the MgO support. The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.5 wt% Pt and 0.25 wt% Sn.

[0054] 9.3 g of catalyst, 1.93 g of magnesium nitrate hexahydrate (Sigma Aldrich), and 2.06 g of deionized water were mixed on a hot plate set to 60°C and stirred until the mixture was dry. The mixture was then heated in air at 110°C for 6 hours and calcined at 800°C for 12 hours. The resulting solid support contained 91 wt% Al2O3 and 9 wt% MgO. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.134 g) (Acros Organics), chloroplatinic acid hexahydrate (0.0244 g) (BioXtra), and deionized water (1 mL) in a small glass vial. This solution was impregnated onto the solid support. The impregnated material was dried in air at 110°C for 6 hours and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn. Catalyst 10: The catalyst was prepared according to the following procedure. 20 g of PURALOX® MG70 / 170 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 70 wt% MgO and 30 wt% Al2O3. According to Sasol, the BET surface area was 170 m². 2 The concentration was / g. An appropriate amount of silver nitrate, tetraammineplatinum(II) nitrate, and deionized water were mixed to form a solution. This solution was impregnated into a PURALOX® MG70 / 170 support. The impregnated material was stored in a sealed container at room temperature for 1 hour, then dried overnight in air at 120°C, and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Ag. Catalyst 11: The catalyst was prepared according to the following procedure. 20 g of PURALOX® MG70 / 170 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 70 wt% MgO and 30 wt% Al2O3. According to Sasol, the BET surface area was 170 m². 2The concentration was / g. An appropriate amount of copper nitrate trihydrate, tetraammineplatinum(II) nitrate, and deionized water were mixed to form a solution. This solution was impregnated into a PURALOX® MG 70 / 170 carrier. The impregnated material was stored in a sealed container at room temperature for 1 hour, then dried overnight in air at 120°C and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Cu.

[0055] Catalyst 12: The catalyst was prepared according to the following procedure. 20 g of PURALOX® MG70 / 170 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 70 wt% MgO and 30 wt% Al2O3. According to Sasol, the BET surface area was 170 m². 2 The concentration was / g. An appropriate amount of gallium(III) nitrate, tetraammineplatinum(II) nitrate, and deionized water were mixed to form a solution. This solution was impregnated into a PURALOX® MG70 / 170 support. The impregnated material was stored in a sealed container at room temperature for 1 hour, then dried overnight in air at 120°C, and calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Ga. Catalyst 13: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.054g) (Acros Organics), chloroplatinic acid hexahydrate (0.0184g) (BioXtra), and deionized water (1.725mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 0.75 wt% Sn. Catalyst 14: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.103g) (Acros Organics), chloroplatinic acid hexahydrate (0.0184g) (BioXtra), and deionized water (1.725mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn.

[0056] Catalyst 15: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.214g) (Acros Organics), chloroplatinic acid hexahydrate (0.0184g) (BioXtra), and deionized water (1.725mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 3.0 wt% Sn. Catalyst 16: The catalyst was prepared according to the following procedure. 5 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m².2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.100g) (Acros Organics), chloroplatinic acid hexahydrate (0.04g) (BioXtra), and deionized water (3.75mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 0.67 wt% Sn. Catalyst 17: KNO3 (0.00812 g) was mixed with deionized water (0.7 mL) in a small glass vial to prepare a solution. This solution was used to impregnate catalyst 16 (1.5 g). The impregnated material was dried in air at 110°C for 6 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt, 0.67 wt% Sn, and 0.21 wt% K.

[0057] Catalyst 18: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.103g) (Acros Organics), chloroplatinic acid hexahydrate (0.0307g) (BioXtra), and deionized water (1.725mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was dried in air at 100°C for 10 hours and then calcined at 800°C for 15 hours. The final product nominally contained 0.5 wt% Pt and 1.5 wt% Sn. Catalyst 19: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. A solution was prepared by mixing tin(IV) chloride pentahydrate (0.103g) (Acros Organics), chloroplatinic acid hexahydrate (0.0187g) (BioXtra), and deionized water (1.725mL) in a small glass vial. This solution was impregnated into a PURALOX® MG80 / 150 support. The impregnated material was dried in air at 100°C for 10 hours and then calcined at 800°C for 15 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn. Catalyst 20: The catalyst was prepared according to the following procedure. 2.3 g of PURALOX® MG80 / 150 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 80 wt% MgO and 20 wt% Al2O3. According to Sasol, the BET surface area was 150 m². 2 The concentration was / g. PURALOX® MG80 / 150 carrier was transferred to a 200 mL beaker filled with 80 mL of deionized water. The mixture was stirred to form slurry A. Solution A was formed by mixing tin(II) chloride dihydrate (0.0663 g) (Sigma Aldrich) with fuming HCl (2 mL). Solution B was formed by mixing chloroplatinic acid hexahydrate (0.0307 g) (BioXtra) with deionized water (10 mL). Solution A and Solution B were mixed to form amber-colored solution C. Solution C was added dropwise to slurry A and stirred for 45 minutes. The resulting mixture was filtered to form a filter cake, which was washed three times with plenty of deionized water. Both the supernatant and wastewater from washing the filter cake were colorless. The filter cake was dried in air at 100°C for 10 hours and then baked at 800°C for 15 hours. The final product nominally contained 0.5 wt% Pt and 1.5 wt% Sn.

[0058] A 1 / 1 (wt / wt) Mg / Al mixed metal oxide support was prepared by dissolving catalyst 21: Mg(NO3)2·6H2O (44.58g) (Sigma-Aldrich) and Al(NO3)3·9H2O (51.55g) (Sigma-Aldrich) in deionized water (100g). The solution was stirred at 70°C and the water was evaporated until solid formation began. This material was then calcined entirely in air at 200°C for 4 hours, and then at 800°C for 4 hours. Finally, this material was ball-milled in an agate cup at 500 rpm for 2 hours to obtain the support. In a glass vial, 0.1280 g of chloroplatinic acid hexahydrate (Sigma Aldrich) and 0.0998 g of tin(II) chloride dihydrate (Fluka) were dissolved in 10.4960 g of deionized water to obtain a clear, deep orange solution. 13.3279 g of Mg / Al mixed metal oxide support was transferred to a 50 mL plastic bottle, to which 9.8957 g of Pt / Sn solution was added. This material was mixed using a small laboratory shaker until a homogeneous, pale orange powder was obtained. This metal-impregnated material was calcined entirely in air at 120°C for 4 hours, and then at 800°C for 12 hours. The final product nominally contained 0.33 wt% Pt and 0.33 wt% Sn. A 0.5 / 1 (wt / wt) Mg / Al mixed metal oxide support was prepared by dissolving catalyst 22: Mg(NO3)2·6H2O (31.89g) (Sigma-Aldrich) and Al(NO3)3·9H2O (73.64g) (Sigma-Aldrich) in deionized water (25.47g). The solution was stirred at 70°C and the water was evaporated until solid formation began. This material was placed in a 120°C oven for 1 hour to further evaporate the water. The dried material was calcined in air at 200°C for 4 hours, then at 800°C for 4 hours. Finally, the calcined material was ball-milled in an agate cup at 500 rpm for 2 hours to obtain the support. In a glass vial, 0.1727 g of chloroplatinic acid hexahydrate (Sigma Aldrich) and 0.1313 g of tin(II) chloride dihydrate (Fluka) were dissolved in 10.7014 g of deionized water to obtain a clear, deep orange solution. 14.2533 g of Mg / Al mixed metal oxide support was transferred to a 50 mL plastic bottle, to which 8.0550 g of Pt / Sn solution was added. This material was mixed using a small laboratory shaker until a homogeneous, pale orange powder was obtained. The metal-impregnated material was calcined in air at 120°C for 4 hours, and then at 800°C for 12 hours. The final product nominally contained 0.33 wt% Pt and 0.33 wt% Sn.

[0059] A 2 / 1 (wt / wt) Mg / Zr mixed metal oxide support was prepared by dissolving Catalyst 23: Zirconium(IV) oxynitrate hydrate (3.69 g) (Sigma-Aldrich) in deionized water (40 g) at 50°C. Mg(NO3)2·6H2O (12.55 g) (Sigma-Aldrich) was added to this solution. The mixture was stirred at 70°C and the water was evaporated until a solid began to form. This material was then calcined entirely in air at 200°C for 4 hours, and then at 800°C for 4 hours, to obtain the support. In a glass vial, 0.0212 g of chloroplatinic acid hexahydrate (Sigma Aldrich) and 0.0318 g of tin(IV) chloride (Sigma Aldrich) were dissolved in 0.6647 g of deionized water to obtain a clear, deep orange solution. 2.0412 g of Mg / Zr mixed metal oxide support was transferred to a 50 mL plastic bottle, to which 0.6007 g of Pt / Sn solution was added. This material was mixed using a small laboratory shaker until a homogeneous, pale orange powder was obtained. The entire metal-impregnated catalyst was dried in air at 120°C for 4 hours, and then calcined at 800°C for 12 hours. The final product nominally contained 0.33 wt% Pt and 0.33 wt% Sn. To prepare a 24:2 / 1 (wt / wt) Mg / Ti mixed metal oxide support catalyst, 8.04 g of MgO (Acros), 4.02 g of TiO2 (Anatase, Sigma Aldrich), and 10 g of H2O were added to an agate ball mill cup along with three agate balls. The material was ball-milled at 500 rpm for 70 hours. The lid was closed during ball milling to minimize water evaporation. After ball milling, a concentrated paste was obtained. This paste was baked at 200°C for 4 hours, then at 800°C for 4 hours to obtain the support catalyst. In a glass vial, 0.0288 g of chloroplatinic acid hexahydrate (Sigma Aldrich) and 0.0336 g of tin(IV) chloride pentahydrate (Sigma Aldrich) were dissolved in 1.6007 g of H2O to obtain a clear, deep orange solution. 2.7321 g of Mg / Ti mixed metal oxide support was transferred to a 50 mL plastic bottle, and the 1.4080 g of Pt / Sn solution prepared above was added dropwise. This material was mixed using a small laboratory shaker until a homogeneous, pale orange powder was obtained. This metal-impregnated catalyst was dried at 120°C for 4 hours and then calcined at 800°C for 12 hours. The final product nominally contained 0.33 wt% Pt and 0.33 wt% Sn.

[0060] Catalyst 25: A 2 / 1 (wt / wt) Mg / Si mixed metal oxide was prepared by adding MgO (8.04g) (Acros), SiO2 (4.03g) (Sigma-Aldrich), deionized water (10g), and three agate balls in an agate ball mill cup. The material was ball-milled at 500 rpm for 70 hours. The lid was closed during ball milling to minimize water evaporation. After ball milling, a concentrated paste was obtained. This paste was calcined entirely in air at 200°C for 4 hours, and then at 800°C for 4 hours, to obtain a support. In a glass vial, 0.0296 g of chloroplatinic acid hexahydrate (Sigma Aldrich) and 0.0365 g of tin(IV) chloride pentahydrate (Sigma Aldrich) were dissolved in 1.4319 g of deionized water to obtain a clear, dark orange solution. 2.8178 g of 1 / 2 Mg / Si mixed metal oxide support was added to a 50 mL plastic bottle, and then 1.2704 g of Pt / Sn solution was added dropwise. This material was mixed using a small laboratory shaker until a homogeneous, pale orange powder was obtained. The entire metal-impregnated catalyst was dried in air at 120°C for 4 hours, and then calcined at 800°C for 12 hours. The final product nominally contained 0.33 wt% Pt and 0.33 wt% Sn. A mixed metal oxide support of Mg / Ca / Sn / Al was prepared by thoroughly mixing catalyst 26: MgO (23.4g) (Aldrich), SnO2 (1.56g) (Aldrich), calcium aluminate cement (12.8g) (Almatis), and Al2O3 (60.5g) (Versal 300). An aqueous acetic acid solution was prepared by adding 10.24 mL of acetic acid to 100 mL of deionized water. An aliquot of 60.4 mL was taken from this solution, and an additional 0.5 mL of acetic acid was added to this aliquot. The aliquots were added to the powder in 5 mL increments, stirring for 2 minutes between additions, until all was used. Deionized water was then added to the mixture until a slurry was formed. The slurry was then calcined in air at 300°C for 20 hours, and then at 843°C for 5 hours to obtain the support. The support prepared above was impregnated with 0.3 wt% Pt and a further 0.3 wt% Sn to obtain the final catalyst. Catalyst 27: The catalyst was prepared according to the following procedure. 20 g of PURALOX® MG70 / 170 (Sasol), a mixed metal oxide of MgO-Al2O3 obtained by calcining hydrotalcite, was secured. The mixed metal oxide contained 70 wt% MgO and 30 wt% Al2O3. According to Sasol, the BET surface area was 170 m². 2The concentration was / g. An appropriate amount of tin(II) chloride dihydrate and deionized water were mixed to form a solution. This solution was impregnated into a PURALOX® MG70 / 170 carrier. The impregnated material was stored in a sealed container at room temperature for 1 hour, and then dried overnight at 120°C. An appropriate amount of tetraammineplatinum(II) nitrate and deionized water were mixed to form a solution. This Pt solution was further impregnated into the Sn-impregnated carrier. The impregnated material was left in a sealed container at room temperature for 1 hour, then dried overnight in air at 120°C, and then calcined at 800°C for 12 hours. The final product nominally contained 0.3 wt% Pt and 1.5 wt% Sn.

[0061] Catalyst compositions 28-41 were prepared according to the following procedure. Each catalyst composition contained 80 wt% MgO and 20 wt% Al2O3, and 150 ml 2 A support was formed by calcining PURALOX® MG 80 / 150 (3 grams) (Sasol), a mixed Mg / Al metal oxide with a surface area of ​​1 / g, at 550°C for 3 hours under air. A solution containing an appropriate amount of tin(IV) chloride pentahydrate (for use in preparing the catalyst composition (Acros Organics)) and / or an appropriate amount of chloroplatinic acid (for use in preparing the catalyst composition (Sigma Aldrich)) and 1.8 ml of deionized water was prepared in a small glass vial. The calcined PURALOX® MG 80 / 150 support (2.3 grams) for each catalyst composition was impregnated with the corresponding solution. The impregnated material was equilibrated in a sealed container at room temperature (RT) for 24 hours, dried at 110°C for 6 hours, and calcined at 800°C for 12 hours. Table 1 shows the nominal Pt and Sn content of each catalyst composition based on the mass of the support.

[0062] [Table 1]

[0063] Comparative Catalyst 1: In a graduated cylinder, 0.048 g of SnCl2 (Aldrich), 0.79 g of an 8% solution of chloroplatinic acid (Aldrich), and the remaining 1.2 M of HCl (Acculute) were mixed to prepare 5.6 mL of Dark solution. This solution was added to 10 g of θ-alumina and stirred for 15 minutes. The catalyst was left to stand for 1 hour. The catalyst was placed in a muffle furnace and heated to 120°C at a rate of 3°C / min in air, maintained at 120°C for 2 hours, and then the catalyst temperature was raised to 550°C at a rate of 3°C / min and maintained for 2 hours. The catalyst was then allowed to cool to room temperature. In a graduated cylinder, 0.258 g of KNO3 (Aldrich) was dissolved in deionized water to obtain a 5.6 mL solution. This solution was added to the Pt-Sn catalyst and stirred for 15 minutes. The catalyst was left to stand for 1 hour. The catalyst was placed in a muffle furnace and heated to 120°C at a rate of 3°C / min in air, maintained at 120°C for 2 hours, and then the catalyst temperature was raised to 550°C at a rate of 3°C / min and maintained for 2 hours. The catalyst was then allowed to cool to room temperature. The final product nominally contained 0.3 wt% Pt, 0.3 wt% Sn, and 1.0 wt% K.

[0064] Examples using the above catalyst Fixed-bed experiments were conducted at an absolute pressure of approximately 100 kPa. The composition of the reactor effluent was measured using gas chromatography (GC). Next, the yield and selectivity of C3H6 were calculated using the concentrations of each component in the reactor effluent. The yield and selectivity of C3H6 reported in these examples were calculated on a carbon molar basis. In each embodiment, a specific amount of catalyst "Mcat" was mixed with an appropriate amount of quartz diluent and packed into a quartz reactor. The amount of diluent was determined so that the catalyst bed (catalyst + diluent) overlapped with the isothermal zone of the quartz reactor and that the catalyst bed remained mostly isothermal during operation. The reactor's dead volume was filled with quartz chips / rods. The yield and selectivity of C3H6 were calculated using the concentrations of each component in the reactor effluent. The data table below shows the results for t rxn At the start and t rxn The yield and selectivity of C3H6 at the end of the process are determined by Y, respectively. ini , Y end S ini , and Send It should be expressed as such and reported as a percentage.

[0065] Example 1 - Effects of exposing spent catalyst to steam at 800°C before oxidation. In Step 1, the effects of exposing spent catalyst to steam were evaluated using two options (Option A and Option B). These are referred to as Case 1A and Case 1B, respectively. The process steps were as follows: 1. (Option A / Case 1A) - The reaction zone was oxidized at temperature T oxi An inert gas was passed through the system while heating it to a certain temperature. Then, 46.6 sccm of He and 5.1 sccm of water vapor were passed through the reaction zone for 5 minutes. 1. (Option B / Case 1B) - The reaction zone was heated to an oxidation temperature T oxi An inert gas was flowed through the system while heating it to [temperature]. Then, 46.6 sccm of He was passed through the reaction zone for 5 minutes. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing the inert gas through the reaction zone, the H2-containing gas (Hgas) was changed to a flow rate (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxnThe hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. As shown in Table 2 below, comparing Case 1A using option A with Case 1B using option B, it can be seen that the performance of the catalyst was not affected even when the spent catalyst was exposed to steam at 800°C before oxidation.

[0066] [Table 2]

[0067] Example 2 - Effects of exposing spent catalyst to steam at 670°C before oxidation. In Step 8, the effects of exposing spent catalyst to steam were evaluated using two options (Option A and Option B). These are referred to as Case 2A and Case 2B, respectively. The process steps were as follows: 1. The reaction zone was oxidized at temperature T oxi 1. While heating up to a certain temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced into the bypass of the reaction zone at a flow rate (F oxi ) was passed through. 3. Next, an oxygen-containing gas was introduced into the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T redThe reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing gas (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn ) was passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. GC sampling was started immediately after switching the feed from the bypass to the reaction zone. 8. (Option A) 46.6 sccm of He and 5.1 sccm of water vapor were passed through the reaction zone for 5 minutes. 8. (Option B) 46.6 sccm of He was passed through the reaction zone for 5 minutes. The above process steps were repeated periodically until stable performance was obtained. As shown in Table 3 below, comparing Case 2A using Option A with Case 2B using Option B, it can be seen that the performance of the catalyst was not affected even when the spent catalyst was exposed to water vapor at 670°C before oxidation.

[0068] [Table 3]

[0069] Example 3A - Preferred oxidation temperature / duration. The process steps were as follows: 1. The reaction zone is oxidized at temperature T. oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing the inert gas through the reaction zone, the H2-containing gas (Hgas) was changed to a flow rate (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained.

[0070] [Table 4]

[0071] Example 3B - Preferred oxidation temperature / duration. The process steps were as follows: 1. The reaction zone is oxidized at temperature T. oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing the inert gas through the reaction zone, the H2-containing gas (Hgas) was changed to a flow rate (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T redThe reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. GC sampling of the reaction effluent was started immediately after switching the feed from the bypass to the reaction zone. Tables 4A, 4B-1, and 4B-2 show that longer oxidation durations resulted in more effective catalyst regeneration. Table 4B-3 shows that higher oxidation temperatures of 800°C or 850°C were more effective than 750°C. For example, the time required to achieve similar yield / selectivity using an oxidation temperature of 750°C was three times longer than required at 800°C.

[0072] [Table 5]

[0073] [Table 6]

[0074] [Table 7]

[0075] Example 4 - Effects of O2 partial pressure and the presence of CO2. The process steps were as follows: 1. The reaction zone is oxidized at temperature T. oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T redChanged to: 5. While passing an inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone was then bypassed for a specific period of time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 5 shows the effect of the partial pressure of O2 on oxidation and the effect of the presence of CO2 on oxidation.

[0076] [Table 8]

[0077] Example 5 - Effect of water vapor during oxidation. The process steps were as follows: 1. The reaction zone was oxidized to temperature T oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. Inert gas was introduced into the system. 6. While passing the inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F redThe reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed over the course of the process. 7. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 8. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 6 shows that the presence of more than 10 vol% water vapor in the air during oxidation resulted in a more deactivated catalyst after regeneration. The more water vapor present in the air during oxidation, the lower the activity. On the other hand, when the humid air was switched to dry air after 2 minutes of oxidation, the catalyst was efficiently regenerated.

[0078] [Table 9]

[0079] Example 6A - Effect of water vapor during oxidation. 1. An inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi The reaction zone was bypassed using ) . The reaction zone was oxidized to oxidation temperature T oxi It was heated to this point. 3. Next, an oxygen-containing gas was introduced into the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the t. oxi Next, while maintaining the oxygen-containing gas flow, the temperature in the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 4. Inert gas was introduced into the system. 5. While passing the inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F redThe reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 7A shows the effect of the presence of water vapor during oxidation. The shorter the duration of contact between the catalyst and water vapor (1 minute vs. 3 minutes), the easier it was for the catalyst performance to recover through subsequent oxidation with dry air.

[0080] [Table 10]

[0081] Example 6B - Effect of water vapor during oxidation. 1. An inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi The reaction zone was bypassed using ) . The reaction zone was oxidized to oxidation temperature T oxi It was heated to this point. 3. Next, an oxygen-containing gas was introduced into the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the t. oxi Next, while maintaining the oxygen-containing gas flow, the temperature in the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 4. Inert gas was introduced into the system. 5. While passing the inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T redWithin the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 655°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 655°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 7B shows that when using a two-step oxidation scheme consisting of 1 minute of moist air oxidation followed by 10 minutes of dry air oxidation, the negative effect of moist air on oxidation was negligible. Figure 1 shows that the catalyst can be efficiently regenerated by using this two-step oxidation scheme for 80+ cycles.

[0082] [Table 11]

[0083] Example 7 - Effect of reduction temperature. 1. An inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone. During this process, the temperature of the reaction zone was changed to the oxidation temperature (T oxi ) change to T oxi at a specific time (t oxi The catalyst was oxidized by maintaining the temperature over a certain period. oxi Next, the temperature within the reaction zone is set to T oxi From reduction temperature (T red ) was changed. 4. Inert gas was introduced into the system. 5. While passing the inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F redThe reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 8 shows that reduction can be performed at various temperatures. A short reduction duration of as little as 0.05 minutes can be utilized.

[0084] [Table 12]

[0085] Example 8 - Effect of water vapor during reduction. 1. The reaction zone was set to oxidation temperature T. oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. A hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through the reaction zone at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 9 shows that the adverse effect of water vapor on the effectiveness of reduction increases with the amount of water vapor in the reducing gas.

[0086] [Table 13]

[0087] Example 9 - Effects of hydrocarbons during reduction. 1. The reaction zone was set to oxidation temperature T. oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T redThe reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 10 shows the adverse effects of trace amounts of hydrocarbons on the effectiveness of reduction.

[0088] [Table 14]

[0089] Example 10 - Reduction of a wet solid. 1. The reaction zone is oxidized at temperature T oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is set to T oxi From reduction temperature (T red ) was changed. Step 5 was performed with one of the following three options to evaluate the effectiveness of reducing the wet solid. 5. (Option 1 / Case 5A) - 83.9 sccm of He was passed through the reaction zone while H2-containing gas (Hgas) was flowed at a flow rate (F red The reaction zone bypass was passed through the gas for 1.5 minutes. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed over the ). 5. (Option 2 / Case 5B) - While passing 3.9 sccm of He and 9.2 sccm of water vapor through the reaction zone, H2-containing gas (Hgas) was flowed at a flow rate (F redThe reaction zone bypass was passed through for 1.5 minutes. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed over a certain distance. 5. (Option 3 / Case 5C) - H2-containing gas (Hgas) was flowed at a velocity (F red The reaction zone was passed through a bypass for 3.0 minutes. During this time, 83.9 sccm of He and 9.2 sccm of water vapor were passed through the reaction zone for the first 1.5 minutes, and then 89.3 sccm of He was passed through the reaction zone for the next 1.5 minutes. After this, the H2-containing gas was passed through the bypass. red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 11 shows the results for cases 5A to 5C. A comparison of cases 5A and 5B shows that reduction of the oxidation catalyst by adsorbed H2O is not effective. A comparison of cases 5B and 5C suggests that adsorbed H2O can be removed by drying gas purging. This re-dried catalyst can then be efficiently reduced by H2.

[0090] [Table 15]

[0091] Example 11 - Effect of water vapor on reduction catalyst. 1. The reaction zone was set to oxidation temperature T. oxi 1. While heating to the temperature, an inert gas was flowed through the system. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red Changed to: 5. While passing an inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone was then bypassed for a specific period of time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) flowed over 6.t red Next, 111.8 sccm of He is passed through the reaction zone with or without an additional 12.3 sccm of water vapor, during which time the temperature of the reaction zone is raised to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 12 shows the effect of the presence of water vapor on the reduction catalyst.

[0092] [Table 16]

[0093] Example 12 - Effect of cooling after reduction. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. An oxygen-containing gas (Ogas) was flowed through the reaction zone at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxiThe catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 800°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the 800°C reaction zone for a specific time (t red ) was flowed over a certain distance. 6. Various flow velocities (F he He was passed through the reaction zone. During this process, the temperature of the reaction zone was lowered from 800°C to 670°C. he The higher the value, the faster the cooling rate (R c ) resulted. The cooling rate is defined as the temperature drop during the first minute of cooling. 7. A hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through the reaction zone at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 13 shows that, after reduction, it may be desirable to cool the reduction catalyst quickly in order to maintain high activity.

[0094] [Table 17]

[0095] Example 13 - Effect of H2 partial pressure during reduction. 1. An inert gas was flowed through the system while the reaction zone was heated to the oxidation temperature of 800°C. 2. An oxygen-containing gas (Ogas) was introduced into the reaction zone at a flow rate (F) while the inert gas was passed through the reaction zone. oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxiThe catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 800°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the 800°C reaction zone for a specific time (t red ) was flowed over 6. He was passed through the reaction zone. During this process, the temperature of the reaction zone was lowered from 800°C to the reaction temperature of 670°C. 7. A hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through the reaction zone at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 14 shows that there is almost no difference between 10% H2 and 40% H2.

[0096] [Table 18]

[0097] Example 14: Effect of A-H2 reduction duration. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 800°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the 800°C reaction zone for a specific time (t red) was flowed over 6. He was passed through the reaction zone. During this process, the temperature of the reaction zone was lowered from 800°C to the reaction temperature of 670°C. 7. A hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through the reaction zone at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 15A shows that there is almost no difference in reduction duration in terms of catalyst performance.

[0098] [Table 19]

[0099] Example 14: Effect of B-H2 reduction duration. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 800°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the 800°C reaction zone for a specific time (t red ) was flowed over 6. He was passed through the reaction zone. During this process, the temperature of the reaction zone was lowered from 800°C to the reaction temperature of 655°C. 7. A hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through the reaction zone at a flow rate (F rxnThe hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 655°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 15B shows that, if catalytic reduction did not occur, the propylene yield of the oxidation catalyst (53.7%) was even lower than the propylene yield of the deactivated catalyst (61.3%).

[0100] [Table 20]

[0101] Example 15 - Effects of exposing spent catalyst to inert gas at 800°C. 1. An inert gas was flowed through the system while the reaction zone was heated to the oxidation temperature of 800°C. Step 2 was performed using one of the following two options to evaluate the effects of exposing spent catalyst to inert gas at 800°C. 2. (Option 1 / Case 15A) An oxygen-containing gas (Ogas) was flowed through the reaction zone at a flow rate (F) while He was passed through the reaction zone for 1 minute. oxi ) was passed through the bypass of the reaction zone for 1 minute. 2. (Option 2 / Case 15B) While passing He through the reaction zone for 7 minutes, oxygen-containing gas (Ogas) was flowed at a flow rate (F oxi ) was passed through the bypass of the reaction zone for 3 minutes. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F red The reaction zone bypass was passed through a specific time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T redThe reaction temperature was changed from [temperature value] to 670 °C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing (HCgas) feed containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% steam was passed through the bypass of the reaction zone at a flow rate (F rxn ) for a specific time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670 °C for 10 minutes. Immediately after switching the feed from the bypass of the reaction zone to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 16 shows that for these two cases, there is little difference in the performance of the catalyst.

[0102]

Table 21

[0103] Example 16 - dehydrogenation of n-butane. 1. An inert gas was flowed through the system while heating the reaction zone to an oxidation temperature of 800 °C. 2. While passing an inert gas through the reaction zone, an oxygen-containing gas (Ogas) was passed through the bypass of the reaction zone at a flow rate (F oxi ). 3. Next, the oxygen-containing gas was passed through the reaction zone for a specific time (t oxi ) to oxidize the catalyst. 4. After t oxi , an inert gas was passed through the reaction zone, and the temperature in the reaction zone was changed from T oxi to a reduction temperature (T red ). 5. While passing an inert gas through the reaction zone, a H2-containing gas (Hgas) was passed through the bypass of the reaction zone at a flow rate (F red ) for a specific time. Thereafter, the H2-containing gas was flowed through the reaction zone at T red for a specific time (t red ). 6. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was changed from T red to a reaction temperature of 635 °C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing (HCgas) feed containing 89 vol% n-butane and 11 vol% steam was passed at a flow rate (F rxn) was passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 635 °C for 10 minutes. GC sampling of the reaction effluent was initiated immediately after switching the feed from the bypass of the reaction zone to the reaction zone. The above process steps were repeated periodically until stable performance was obtained. The catalyst did not show deactivation after 30+ cycles. Since no internal standard was used during this experiment, species that were not analyzed by GC (C5 and C 5+ , coke) were assumed to be negligible in order to calculate selectivity and yield. The fact that no large amount of coke was generated during the reaction was confirmed by the small amount of CO / CO2 generated during oxidation. Yield / selectivity is defined based on the molar flow rates of all major linear C4 species generated during the reaction, such as 1-butene, cis-2-butene, trans-2-butene, 1,3-butadiene, etc. Table 17 shows that the catalyst is effective for the dehydrogenation of n-butane.

[0104]

Table 22

[0105] Example 17 - Dehydrogenation of isobutane. 1. An inert gas was flowed through the system while heating the reaction zone to an oxidation temperature of 800 °C. 2. While passing an inert gas through the reaction zone, an oxygen-containing gas (Ogas) was passed through the bypass of the reaction zone at a flow rate (F oxi ). 3. Next, the oxygen-containing gas was passed through the reaction zone for a specific time (t oxi ) to oxidize the catalyst. 4. After t oxi , an inert gas was passed through the reaction zone and the temperature in the reaction zone was changed from T oxi to the reduction temperature (T red ). 5. While passing an inert gas through the reaction zone, a H2-containing gas (Hgas) was passed through the bypass of the reaction zone at a flow rate (F red ) for a specific period of time. After that, the H2-containing gas was flowed through the reaction zone at T red for a specific time (t red ). 6. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was T redThe reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 89 vol% isobutane and 11 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. The catalyst did not show deactivation after 30+ cycles. Since no internal standards were used during this experiment, species not analyzed by GC (C5 and C5) were used to calculate selectivity and yield. 5+ It was assumed that coke could be ignored. The absence of large amounts of coke during the reaction was confirmed by the small amount of CO / CO2 produced during oxidation. Yield / selectivity is defined based on the molar flow rate of isobutene produced during the reaction. Table 18 shows that the catalyst is effective for the dehydrogenation of isobutane. Figure 2 shows that the dehydrogenation of isobutane was stable for this catalyst over 30+ cycles, despite the use of high temperatures during the reaction, reduction, and oxidation.

[0106] [Table 23]

[0107] Example 18 - Dehydrogenation of ethane. 1. An inert gas was flowed through the system while the reaction zone was heated to the oxidation temperature of 800°C. 2. An oxygen-containing gas (Ogas) was introduced into the reaction zone at a flow rate (F) while the inert gas was passed through the reaction zone. oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F redThe reaction zone was then bypassed for a specific period of time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C2H6, 9 vol% Ar, and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. GC sampling of the reaction effluent was started immediately after switching the feed from the bypass to the reaction zone. The above process steps were repeated periodically until stable performance was obtained. The catalyst did not show deactivation after 30+ cycles. Table 19 shows that the catalyst is effective for the dehydrogenation of ethane. When the catalyst in the reaction zone was replaced with quartz, the measured C2H4 yield was less than 1 C mol%. This indicates that there was little homogeneous reaction under these test conditions.

[0108] [Table 24]

[0109] Example 19 - Effect of the support. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. An oxygen-containing gas (Ogas) was flowed through the reaction zone at a flow rate (F) while the inert gas was passed through the reaction zone. oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 800°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the 800°C reaction zone for a specific time (t red) was flowed over 6. He was passed through the reaction zone. During this process, the temperature of the reaction zone was lowered from 800°C to the reaction temperature of 670°C. 7. A hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through the reaction zone at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 20 shows that catalysts with high activity / selectivity / stability can be produced using various Mg-containing catalyst supports.

[0110] [Table 25]

[0111] Figure 3 shows that the performance of catalyst 6 remained stable over 30+ cycles despite the high temperatures used during the reaction, reduction, and oxidation. Example 20 - Effect of the support. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. An oxygen-containing gas (Ogas) was flowed through the reaction zone at a flow rate (F) while the inert gas was passed through the reaction zone. oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the system. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was cooled to 620°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the reaction zone at 620°C for a specific time (t red) was flowed over 6. Inert gas was passed through the reaction zone. During this process, the temperature of the reaction zone was maintained at 620°C. 7. While passing inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 620°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 21 shows that catalysts with high activity / selectivity / stability can be produced using various Mg-containing catalyst supports.

[0112] [Table 26]

[0113] Figure 4 shows that the performance of catalyst 8 remained stable for 20+ cycles despite the high temperatures used during the reaction, reduction, and oxidation. Figure 5 shows that the performance of catalyst 9 remained stable for 30+ cycles with respect to this catalyst, despite the high temperatures used during the reaction, reduction, and oxidation. Example 21 - Effect of metal accelerator. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F red The reaction zone was then bypassed for a specific period of time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (tred ) was flowed over 6. Inert gas was flowed into the reaction zone. During this process, the temperature of the reaction zone was changed to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 22 shows that metals other than Sn can be used with Pt for dehydrogenation.

[0114] [Table 27]

[0115] Example 22 - Effect of Sn level. 1. While passing an inert gas through the reaction zone, oxygen-containing gas (Ogas) was flowed through the bypass of the reaction zone, which was maintained at 670°C, at a flow rate (F oxi ) was passed through. 2. Next, the oxygen-containing gas was passed through the reaction zone while raising the temperature of the reaction zone to 800°C. The oxygen-containing gas was passed through for a specific time (t oxi The catalyst was oxidized by continuously flowing it through the reaction zone over a certain period of time (F). The reaction zone was then cooled to 670°C in an oxygen-containing gas. 3. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 670°C. 4. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F). red The gas was then passed through a bypass of the reaction zone for a specific period of time. After this, the H2-containing gas was passed through the reaction zone at 670°C for a specific period of time (t red) was flowed through. 5. An inert gas was passed through the reaction zone. During this process, the temperature of the reaction zone was maintained at 670 °C. 6. While passing an inert gas through the reaction zone, a hydrocarbon-containing (HCgas) feed containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% steam was passed through the bypass of the reaction zone at a flow rate (F rxn ) for a specific time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670 °C for 10 minutes. Immediately after switching the feed from the bypass of the reaction zone to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeatedly carried out periodically until stable performance was obtained. Table 23 shows that the Sn loading on the catalyst can be varied.

[0116]

Table 28

[0117] Example 23 - Effect of alkali metal additives. 1. While passing an inert gas through the reaction zone, an oxygen-containing gas (Ogas) was passed through the bypass of the reaction zone maintained at 670 °C at a flow rate (F oxi ) 2. Next, while raising the temperature of the reaction zone to 8**00** °C, the oxygen-containing gas was passed through the reaction zone. The oxygen-containing gas was continuously flowed through the reaction zone for a specific time (t oxi ) to oxidize the catalyst. Thereafter, the reaction zone was cooled to 670 °C in the oxygen-containing gas. 3. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 670 °C. 4. While passing an inert gas through the reaction zone, a H2-containing gas (Hgas) was passed through the bypass of the reaction zone at a flow rate (F red ) for a specific time. Thereafter, the H2-containing gas was flowed through the reaction zone at 670 °C for a specific time (t red ) 5. An inert gas was passed through the reaction zone. During this process, the temperature of the reaction zone was maintained at 670 °C. 6. While passing an inert gas through the reaction zone, a hydrocarbon-containing (HCgas) feed containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% steam was passed through the bypass of the reaction zone at a flow rate (F rxn It seems there might be a typo in the original text where "8**00** °C" is shown. I've translated it as it is for the purpose of following the instructions. If this is an error, please correct the original text for a more accurate translation.The hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 24 shows that alkali metals such as K may be added to the catalyst.

[0118] [Table 29]

[0119] Example 24 - Effects of Pt level and synthesis method. 1. An inert gas was flowed through the system while the reaction zone was heated to an oxidation temperature of 800°C. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced at a flow rate (F oxi ) was passed through the bypass of the reaction zone. 3. Next, oxygen-containing gas was passed through the reaction zone for a specific time (t oxi The catalyst was oxidized by passing it through the following path. 4.t oxi Next, an inert gas is passed through the reaction zone, and the temperature inside the reaction zone is raised to T oxi From reduction temperature (T red ) was changed. 5. While passing an inert gas through the reaction zone, the flow rate of H2-containing gas (Hgas) was changed (F red The reaction zone was then bypassed for a specific period of time. After this, the H2-containing gas was introduced into the T red Within the reaction zone, for a specific time (t red ) was flowed through. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was set to T red The reaction temperature was changed from 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) consisting of 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxnThe hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specific period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 25 shows that the amount of Pt loaded on the catalyst and the synthesis method can be varied.

[0120] [Table 30]

[0121] Example 25 - Effect of the support. 1. While passing an inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced into the bypass of the reaction zone, which was maintained at 620°C, at a flow rate (F oxi ) was passed through. 2. Next, the oxygen-containing gas was passed through the reaction zone while raising the temperature of the reaction zone to 800°C. The oxygen-containing gas was passed through for a specific time (t oxi The catalyst was oxidized by continuously flowing it through the reaction zone over a certain period of time (F). The reaction zone was then cooled to 620°C in an oxygen-containing gas. 3. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was maintained at 620°C. 4. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F). red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through the 620°C reaction zone for a specific time (t red ) was flowed over 5. Inert gas was passed through the reaction zone. During this process, the temperature of the reaction zone was maintained at 620°C. 6. While passing inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was passed through at a flow rate (F rxnThe hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 620°C for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained. Table 26 shows that catalysts with good activity, selectivity, and high-temperature stability can be prepared using various Mg-containing catalyst supports.

[0122] [Table 31]

[0123] Example 26 - Effect of the carrier. 1. The reaction zone is T oxi 1. An inert gas was flowed through the system while changing the oxidation temperature. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced into the bypass of the reaction zone at a flow rate (F oxi ) was passed through. 3. Next, the oxygen-containing gas was passed through for a specific time (t oxi The catalyst was oxidized by passing it through the reaction zone over 24 hours. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was changed to T red Changed to: 5. While passing an inert gas through the reaction zone, H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was then passed through for a specific time. After this, the H2-containing gas was passed through for a specific time (t red ) over T red The reaction zone was flowed through. 6. An inert gas was passed through the reaction zone. During this process, the temperature of the reaction zone was changed to T rxn Changed to: 7. Passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert (Ar or Kr), and 10 vol% water vapor was introduced at a flow rate (F rxn The reaction zone bypass was then passed through a specific time. Next, the hydrocarbon-containing feed was passed through T rxnThe feed was passed through the reaction zone for 10 minutes. As soon as the feed was switched from the bypass to the reaction zone, GC sampling of the reaction effluent was started. The above process steps were repeated periodically until stable performance was obtained.

[0124] [Table 32]

[0125] Table 27 above shows that catalysts with good activity, selectivity, and high-temperature stability can be prepared using various Mg-containing catalyst supports. Figure 6 shows that the performance of catalyst 24 remained stable over 20+ cycles despite the high temperatures used during reaction, reduction, and oxidation. Comparative Example 1: 1. The reaction zone is T oxi 1. An inert gas was flowed through the system while heating it to the oxidation temperature. 2. While passing the inert gas through the reaction zone, an oxygen-containing gas (Ogas) was introduced into the bypass of the reaction zone at a flow rate (F oxi ) was passed through. 3. Next, the oxygen-containing gas was passed through for a specific time (t oxi The catalyst was oxidized by passing it through the reaction zone over a certain distance. 4. An inert gas was flowed through the system. During this process, the temperature of the reaction zone was cooled to 620°C. 5. While passing the inert gas through the reaction zone, an H2-containing gas (Hgas) was introduced at a flow rate (F red The reaction zone bypass was passed through for a specific time. After this, the H2-containing gas was passed through for a specific time (t red ) was flowed through a reaction zone at 620°C. 6. Inert gas was passed through the reaction zone. During this process, the temperature of the reaction zone was maintained at 620°C. 7. A hydrocarbon-containing feed (HCgas) containing 90 vol% C3H8 and 10 vol% inert (Ar or Kr) was passed through the reaction zone at a flow rate (F rxnThe hydrocarbon-containing feed was then passed through the bypass of the reaction zone for a specified period of time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 620°C for 10 minutes. GC sampling of the reaction effluent was started immediately after switching the feed from the bypass to the reaction zone. Table 28 shows further details of the test conditions for the comparative example. Figure 7 shows that comparative catalyst 1 continued to deactivate despite the oxidation temperature (620°C) being much lower than that of the other examples.

[0126] [Table 33]

[0127] In Example 27, a fixed-bed experiment using catalysts 28-41 was conducted at an absolute pressure of approximately 100 kPa. The composition of the reactor effluent was investigated using gas chromatography (GC). Next, the yield and selectivity of C3H6 were calculated using the concentrations of each component in the reactor effluent. The yield and selectivity of C3H6 reported in these examples were calculated on a carbon molar basis. In each example, 0.3 g of the catalyst composition was mixed with an appropriate amount of quartz diluent and packed into a quartz reactor. The amount of diluent was determined so that the catalyst bed (catalyst + diluent) overlapped with the isothermal zone of the quartz reactor and the catalyst bed remained nearly isothermal during operation. The dead volume of the reactor was filled with quartz chips / rods. Tables 29 and 30 below, relating to catalysts 28-35, rxn At the start and t rxn The yield and selectivity of C3H6 at the end of the process are determined by Y, respectively. ini , Y end S ini , and S end It is expressed as such and reported as a percentage. The process steps for catalysts 28-35 were as follows: 1. Inert gas was flowed through the system. 2. Dry air was passed through the bypass of the reaction zone at a flow rate of 83.9 sccm while the inert gas was passed through the reaction zone. The reaction zone was heated to a regeneration temperature of 800°C. 3. Next, the catalyst was regenerated by passing dry air through the reaction zone at a flow rate of 83.9 sccm for 10 minutes. 4. Inert gas was flowed through the system. 5. While the inert gas was passed through the reaction zone, an H2-containing gas having 10 vol% H2 and 90 vol% Ar was passed through the bypass of the reaction zone at a flow rate of 46.6 sccm for a specific time. After this, the H2-containing gas was passed through the 800°C reaction zone for 3 seconds. 6. Inert gas was flowed through the system. During this process, the temperature of the reaction zone was changed from 800°C to a reaction temperature of 670°C. 7. While passing an inert gas through the reaction zone, a hydrocarbon-containing feed (HCgas) containing 81 vol% C3H8, 9 vol% inert gas (Ar or Kr), and 10 vol% water vapor was passed through the bypass of the reaction zone at a flow rate of 35.2 sccm for a specified time. Next, the hydrocarbon-containing feed was passed through the reaction zone at 670°C for 10 minutes. GC sampling of the reaction effluent was started immediately after switching the feed from the bypass to the reaction zone. The above process steps were repeated periodically until stable performance was obtained. Tables 29 and 30 show that catalyst 33, containing only 0.025 wt% Pt and 1 wt% Sn, exhibited both similar yield and selectivity compared to catalysts containing 0.4 wt% Pt and 1 wt% Sn, which was surprising and unexpected. Catalyst 35, which contained no Pt, did not show a recognizable propylene yield.

[0128] [Table 34]

[0129] [Table 35]

[0130] Catalysts 28-35 were tested using the same process steps 1-7 described above for catalysts 36-41. Table 31 shows that for a catalyst composition containing 0.1 wt% Pt based on the mass of the support, the Sn level should not be too low or too high for the optimal propylene yield.

[0131] [Table 36]

[0132] Table 32 shows that for a catalyst composition containing 0.0125 wt% Pt based on the mass of the support, the level of Sn should not be too high or too low for the optimal propylene yield.

[0133] [Table 37]

[0134] Except for using a flow rate of 17.6 sccm instead of 35.2 sccm in step 7, catalysts 28-35 were subjected to lifetime testing using the same process steps 1-7 described above, and catalyst 33, containing only 0.025 wt% Pt and 1 wt% Sn, was also tested. Figure 8 shows that catalyst 33 maintained its performance over 204 cycles (x axis is time, and y axis is the yield of C3H6 and selectivity for C3H6, both in carbon mole percent).

[0135] List of embodiments This disclosure further includes the following non-limiting embodiments. A1. A regeneration process for at least partially deactivated catalyst comprising a Group 10 element, an inorganic support, and impurities, wherein the Group 10 element has a concentration in the range of 0.001 wt% to 6 wt% based on the mass of the inorganic support, and the process comprises: (I) obtaining a precursor catalyst from the at least partially deactivated catalyst; (II) supplying an oxidizing gas comprising 5 mol% or less of H2O based on its total moles; (III) contacting the precursor catalyst with the oxidizing gas at an oxidation temperature in the range of 620°C to 1,000°C for a duration of at least 30 seconds, preferably at least 1 minute, preferably at least 5 minutes, to produce an oxidized precursor catalyst; and (IV) obtaining a regenerated catalyst from this oxidized precursor catalyst. A2. The process of A1, wherein the Group 10 element is Pt, and the inorganic support contains at least 0.5 wt% of a Group 2 element based on the mass of the inorganic support. A3. The process of A2, wherein the group 2 element includes Mg, and at least a portion of the group 2 element is in the form of MgO or a mixed oxide containing MgO. A4. One of the processes A1 to A3, wherein at least a partially deactivated catalyst further comprises up to 10 wt% of an accelerator based on the mass of an inorganic support, and the accelerator comprises one or more of the following elements: Sn, Ag, Cu, combinations thereof, or mixtures thereof. A5. Any one of the processes A1 to A4, wherein at least a partially deactivated catalyst further comprises up to 5 wt% of an alkali metal element disposed on an inorganic support, and this alkali metal element comprises at least one of Li, Na, K, Rb, and Cs. A6. C2-C of 1 or more types 16 Straight-chain or branched alkanes, or one or more C4-C 16 Cyclic alkanes, one or more C8-C 16 One of the processes A1 to A5, wherein the active component of the regenerative catalyst contains a Group 10 element, and is capable of causing one or more dehydrogenation, dehydrogenated aromatication, and dehydrogenated cyclization of a hydrocarbon-containing feed containing alkyl aromatic hydrocarbons or mixtures thereof. A7. Any one of the processes A1 to A6, wherein step (I) is a heating gas mixture containing H2O at a concentration of more than 5 mol% based on its total moles, to heat a catalyst that is at least partially deactivated to produce a precursor catalyst. A8. The process of A7, wherein the heated gas mixture is produced by burning a fuel with an oxidizing gas, the fuel comprising H2, CO, and at least one hydrocarbon, and the oxidizing gas comprising O2.

[0136] A9. One of the processes A1 to A6, wherein in step (I), a catalyst that is at least partially deactivated is supplied as a precursor catalyst. A10. Any one of the processes A1 to A9, wherein step (II) includes (IIa) supplying an oxidizing gas at a temperature below the oxidation temperature, and (IIb) preheating the oxidizing gas to a temperature higher than the temperature of the precursor catalyst before contact in step (III). A11. Any one of the processes A1 to A10, further comprising the step of heating an oxidizing gas or precursor catalyst by using a radiant heat source, a heat exchanger, or a combination thereof during step (III). A12. One of the processes from A1 to A11, wherein step (IV) includes (IVa) contacting an oxidation precursor catalyst with a first stripping gas that does not contain O2 to produce a stripped oxidation precursor catalyst, and (IVb) obtaining a regenerated catalyst from this stripped oxidation precursor catalyst. A13. Any one of the processes A1 to A12, wherein step (IV) includes (IVc) contacting an oxidation precursor catalyst or a detachment oxidation precursor catalyst with an H2-containing atmosphere to produce a reduction catalyst, and (IVd) obtaining a regenerated catalyst from this reduction catalyst. A14. The process of A13, wherein step (IVd) includes contacting the (IVd-1) reduction catalyst with a second stripping gas to produce a regenerated catalyst. A15. The process of A13 or A14, wherein step (IVc) is performed at a temperature of the oxidation precursor catalyst that is higher than the operating temperature of the regenerated catalyst, and step (IVd) further comprises (IVd-2) cooling the reduction catalyst or regenerated catalyst to the operating temperature for a duration of 10 minutes or less, 5 minutes or less, 1 minute or less, 30 seconds or less, 10 seconds or less, 5 seconds or less, 1 second or less, 0.5 seconds or less, 0.1 seconds or less, 0.01 seconds or less, or 0.001 seconds or less.

[0137] A16. A dehydrogenation process using a regenerating catalyst produced by any one of the processes A1 to A15, the steps being: (VI) Contacting a hydrocarbon-containing feed with the regenerating catalyst to cause one or more of the hydrocarbon-containing feed to undergo dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization, thereby producing at least a partially deactivated catalyst containing a Group 10 element, an inorganic support, and impurities, and an effluent containing one or more upgraded hydrocarbons and molecular hydrogen, wherein the hydrocarbon feed contains one or more C2-C 16 Straight-chain or branched alkanes, one or more C4-C 16 Cyclic alkanes, one or more C8-C 16 A dehydrogenation process comprising: (VII) a step comprising an alkyl aromatic hydrocarbon or a mixture thereof; (VII) a step of repeating steps (I) to (IV), wherein in step (III) an additional oxidation precursor catalyst is generated, and in step (IV) an additional regenerating catalyst is obtained from the additional oxidation precursor catalyst; and (VIII) a step of contacting an additional amount of hydrocarbon-containing feed with at least a portion of the additional regenerating catalyst to generate an additional at least partially deactivated catalyst and additional effluent. A17. The dehydrogenation process of A16, wherein the cycle time from the contact of the hydrocarbon-containing feed with the regenerating catalyst in step (VI) to the contact of the additional hydrocarbon-containing feed with the additional regenerating catalyst in step (VIII) is ≤ 5 hours.

[0138] B1. A hydrocarbon upgrade process, comprising the steps of (I) contacting a hydrocarbon-containing feed with a catalyst comprising a Group 10 element and an inorganic support to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of at least a portion of the hydrocarbon-containing feed to produce at least a partially deactivated catalyst comprising a Group 10 element, an inorganic support, and impurities, and an effluent comprising one or more upgraded hydrocarbons and molecular hydrogen, wherein the hydrocarbon-containing feed comprises one or more C2-C 16 Straight-chain or branched alkanes, one or more C4-C 16 Cyclic alkanes, one or more C8-C 16 A process comprising the steps of: (II) obtaining a precursor catalyst from at least a partially deactivated catalyst; (III) supplying an oxidizing gas, which contains 2 mol% or less of H2O based on its total moles; (IV) contacting the precursor catalyst with the oxidizing gas at an oxidation temperature in the range of 620°C to 1,000°C for a duration of at least 30 seconds, preferably at least 1 minute, preferably at least 5 minutes, to produce an oxidized precursor catalyst; (V) obtaining a regenerated catalyst from the oxidized precursor catalyst; and (VI) contacting at least a portion of the regenerated catalyst with an additional amount of hydrocarbon-containing feed to produce an additional at least partially deactivated catalyst and additional effluents.

[0139] B2. The process of B1, wherein the Group 10 element is Pt, the inorganic support contains at least 0.5 wt% of Group 2 elements based on the mass of the inorganic support, the catalyst optionally further contains up to 10 wt% of an accelerator based on the mass of the inorganic support, the accelerator, if present, contains one or more of the following elements: Sn, Ag, Cu, a combination thereof, or a mixture thereof, and the catalyst optionally further contains up to 5 wt% of an alkali metal element, the alkali metal element, if present, contains at least one of Li, Na, K, Rb, and Cs. B3. The process of B1 or B2, wherein step (II) is a heating gas mixture comprising heating a partially deactivated catalyst to produce a precursor catalyst using a heating gas mixture containing H2O at a concentration of more than 5 mol% based on its total moles. B4. The process of B3, wherein the heated gas mixture is produced by burning a fuel with an oxidizing gas, the fuel comprising H2, CO, and at least one hydrocarbon, and the oxidizing gas comprising O2. B5. One of the processes B1 to B4, in which at least partially deactivated catalyst is supplied as a precursor catalyst in step (II). B6. Any one of the processes B1 to B5, wherein step (III) includes (IIIa) supplying an oxidizing gas at a temperature below the oxidation temperature and (IIIb) preheating the oxidizing gas to a temperature higher than the temperature of the precursor catalyst before contact in step (IV). B7. Any one of the processes from B1 to B6, further comprising the step of heating an oxidizing gas or precursor catalyst by using a radiant heat source, a heat exchanger, or a combination thereof during step (IV). B8. One of the processes from B1 to B7, wherein the cycle time from the contact of the hydrocarbon-containing feed with the catalyst in step (I) to the contact of the hydrocarbon-containing feed with the regenerated catalyst in step (VI) is ≤ 5 hours.

[0140] Various terms have been defined above. Unless a term used in a claim is defined above, the broadest definition given to that term by a person skilled in the art, as reflected in at least one publication and granted patent, should be given. Furthermore, all patents, test procedures, and other documents referenced in this application are incorporated by reference to such an extent that such disclosure is not inconsistent with this application, and are incorporated for all jurisdictions in which such incorporation is permitted. The above description relates to embodiments of the present invention, but other further embodiments of the present invention can be devised without departing from the basic scope of the present invention, the scope of which is defined by the following claims. Another aspect of the present invention may be as follows: [1] A regeneration process for at least partially deactivated catalyst comprising a Group 10 element, an inorganic support, and impurities, wherein the Group 10 element has a concentration in the range of 0.001 wt% to 6 wt% based on the mass of the inorganic support, and the process is (I) A heated gas mixture having a concentration of more than 5 mol% based on its total moles. 2 A step of generating a precursor catalyst by heating the at least partially deactivated catalyst using a heated gas mixture containing O, (II) Oxidizing gases, where H is present in a quantity of 5 mol% or less based on the total moles. 2 The steps include supplying an oxidizing gas containing O, (III) A step of generating an oxidation precursor catalyst by contacting the precursor catalyst with the oxidizing gas at an oxidation temperature in the range of 620°C to 1,000°C for a duration of at least 30 seconds, preferably at least 1 minute, preferably at least 5 minutes, (IV) A step of obtaining a regenerated catalyst from the oxidation precursor catalyst. The process including the process described above. [2] The process according to [1], wherein the heated gas mixture is produced by burning a fuel with an oxidizing gas. [3] The fuel is H 2 The oxidizing gas comprises CO and at least one hydrocarbon, and the oxidizing gas is O 2 The process described in [2] above, including the process described in [2] above. [4] The process according to any one of [1] to [3], wherein the group 10 element includes Pt, and the inorganic support contains at least 0.5 wt% of a group 2 element based on the mass of the inorganic support. [5] The group 2 element includes Mg, The process according to [4], wherein at least a portion of the group 2 element is in the form of MgO or a mixed oxide containing MgO. [6] The process according to any one of the above [1] to [5], wherein the at least partially deactivated catalyst further comprises up to 10 wt% of an accelerator based on the mass of the inorganic support, the accelerator comprising one or more of the following elements: Sn, Ag, Cu, combinations thereof, or mixtures thereof. [7] The process according to any one of [1] to [6], wherein the at least partially deactivated catalyst further comprises up to 5 wt% of an alkali metal element disposed on the inorganic support, the alkali metal element comprising at least one of Li, Na, K, Rb, and Cs. [8] One or more types of C 2 -C 16 Straight-chain or branched alkanes, or one or more carbon atoms. 4 -C 16 Cyclic alkanes, one or more C 8 -C 16 The process according to any one of claims [1] to [7], wherein the active component of the regenerating catalyst is a group 10 element, and the regenerating catalyst is capable of causing one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of a hydrocarbon-containing feed containing alkyl aromatic hydrocarbons or mixtures thereof. [9] Step (II) is, (IIa) The step of supplying the oxidizing gas at a temperature below the oxidation temperature, (IIb) The step of preheating the oxidizing gas to a temperature higher than the temperature of the precursor catalyst before contact in step (III). The process described in any one of the above paragraphs [1] to [8], including the process described in any one of paragraphs [1] to [8].

[10] Furthermore, (V) Step (III) includes heating the oxidizing gas, the precursor catalyst, or both by using a radiant / conductive heat source, a heat exchanger, or a combination thereof. The process described in any one of the above items [1] to [9].

[11] Step (IV) is, (IVa) The oxidation precursor catalyst is O 2 A step of producing a stripping oxidation precursor catalyst by contacting it with a first stripping gas that does not contain, (IVb) A step of obtaining the regenerated catalyst from the exfoliated oxidation precursor catalyst, The process described in any one of the above paragraphs [1] to

[10] , including the process described in any one of paragraphs [1] to

[10] .

[12] Step (IV) is, (IVc) The oxidation precursor catalyst or the exfoliation oxidation precursor catalyst is H 2 A step of generating a reduction catalyst by contacting it with the contained atmosphere, (IVd) A step of obtaining the regenerating catalyst from the reduction catalyst. The process described in any one of the above paragraphs [1] to

[11] , including the process described in any one of paragraphs [1] to

[11] .

[13] Step (IVd) is (IVd-1) A step of generating the regenerated catalyst by contacting the reduction catalyst with a second stripping gas. The process described in

[12] above, including the process described in

[12] above.

[14] Step (IVc) is carried out at a temperature of the oxidation precursor catalyst that is higher than the operating temperature of the regenerated catalyst, and step (IVd) is further, (IVd-2) A step of cooling the reduction catalyst or the regeneration catalyst to the operating temperature for a duration of 10 minutes or less, 5 minutes or less, 1 minute or less, 30 seconds or less, 10 seconds or less, 5 seconds or less, 1 second or less, 0.5 seconds or less, 0.1 seconds or less, 0.01 seconds or less, or 0.001 seconds or less. The process described in

[12] or

[13] above, including the process described above.

[15] A dehydrogenation process using the regenerated catalyst produced by any one of the processes described in [1] to

[14] above, (VI) Contacting a hydrocarbon-containing feed with the regenerating catalyst to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of at least a portion of the hydrocarbon-containing feed to produce the at least partially deactivated catalyst comprising the Group 10 elements, the inorganic support, and the impurities, and an effluent comprising one or more upgraded hydrocarbons and molecular hydrogen, wherein the hydrocarbon feed comprises one or more C 2 -C 16 Straight-chain or branched alkanes, one or more types of carbon 4 -C 16 Cyclic alkanes, one or more C 8 -C 16 A step comprising alkyl aromatic hydrocarbons or a mixture thereof, (VII) A step in which steps (I) to (IV) are repeated, wherein an additional oxidation precursor catalyst is generated in step (III), and an additional regenerating catalyst is obtained from the additional oxidation precursor catalyst in step (IV), (VIII) The step of contacting an additional amount of the hydrocarbon-containing feed with at least a portion of the additional regenerating catalyst to generate an additional at least partially deactivated catalyst and an additional effluent. The dehydrogenation process, including the dehydrogenation process.

[16] The dehydrogenation process according to

[15] , wherein the cycle time from the contact of the hydrocarbon-containing feed with the regenerating catalyst in step (VI) to the contact of the additional amount of hydrocarbon-containing feed with the additional regenerating catalyst in step (VIII) is 5 hours or less.

[17] A hydrocarbon upgrade process, (I) A step of contacting a hydrocarbon-containing feed with a catalyst comprising a Group 10 element and an inorganic support to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of at least a portion of the hydrocarbon-containing feed to produce at least a partially deactivated catalyst comprising the Group 10 element, the inorganic support, and impurities, and an effluent comprising one or more upgraded hydrocarbons and molecular hydrogen, The hydrocarbon-containing feed contains one or more C 2 -C 16 Straight-chain or branched alkanes, or one or more carbon atoms. 4 -C 16 Cyclic alkanes, one or more C 8 -C 16 Containing alkyl aromatic hydrocarbons or mixtures thereof, The group 10 elements have a concentration in the range of 0.001 wt% to 6 wt% based on the mass of the inorganic carrier. The hydrocarbon-containing feed and the catalyst are brought into contact at a temperature in the range of 300°C to 900°C, and The step includes the provision that the one or more upgraded hydrocarbons include at least one of dehydrogenated hydrocarbons, dehydrogenated aromatic hydrocarbons, and dehydrogenated cyclized hydrocarbons, (II) A heated gas mixture having a concentration of more than 5 mol% based on its total moles. 2 A step of generating a precursor catalyst by heating the at least partially deactivated catalyst using a heating gas mixture containing O, (III) Oxidizing gases, where H is present in a total mole amount of 2 mol% or less. 2 The steps include supplying an oxidizing gas containing O, (IV) A step of generating an oxidation precursor catalyst by contacting the precursor catalyst with the oxidizing gas at an oxidation temperature in the range of 620°C to 1,000°C for a duration of at least 30 seconds, preferably at least 1 minute, preferably at least 5 minutes, (V) A step of obtaining a regenerated catalyst from the oxidation precursor catalyst, (VI) The step of contacting an additional amount of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst to generate an additional at least partially deactivated catalyst and additional effluent. The process including the process described above.

[18] The process according to

[17] , wherein the heated gas mixture is produced by burning a fuel with an oxidizing gas.

[19] The fuel is H 2 The oxidizing gas comprises CO and at least one hydrocarbon, and the oxidizing gas is O 2 The process described in

[18] above, including the process described in

[18] above.

[20] The group 10 element includes Pt, The process according to any one of the above

[17] to

[19] , wherein the inorganic support comprises at least 0.5 wt% of a group 2 element based on the mass of the inorganic support.

[21] The process according to any one of the preceding paragraphs

[17] to

[20] , wherein the catalyst further comprises up to 10 wt% of an accelerator based on the mass of the inorganic support, the accelerator comprising one or more of the following elements: Sn, Ag, Cu, combinations thereof, or mixtures thereof.

[22] The process according to any one of

[17] to

[21] , wherein the catalyst further comprises up to 5 wt% of an alkali metal element, the alkali metal element comprising at least one of Li, Na, K, Rb, and Cs.

[23] Step (III) is, (IIIa) The step of supplying the oxidizing gas at a temperature below the oxidation temperature, (IIIb) The step of preheating the oxidizing gas to a temperature higher than the temperature of the precursor catalyst before contact in step (IV), The process described in any one of the preceding paragraphs

[17] to

[22] , including the process described in any one of paragraphs

[17] to

[22] .

[24] Furthermore, (VII) step of heating the oxidizing gas, the precursor catalyst, or both by using a radiant / conductive heat source, a heat exchanger, or a combination thereof during step (IV). The process described in any one of the preceding paragraphs

[17] to

[23] , including the process described in any one of paragraphs

[17] to

[23] .

[25] The process according to any one of the above

[17] to

[24] , wherein the cycle time from the contact of the hydrocarbon-containing feed with the catalyst in step (I) to the contact of the additional amount of hydrocarbon-containing feed with the regenerating catalyst in step (VI) is 5 hours or less.

Claims

1. A regeneration process for at least partially deactivated catalyst comprising a Group 10 element, an inorganic support, and an impurity, wherein the Group 10 element has a concentration in the range of 0.01 wt% to 1 wt% based on the mass of the inorganic support, the Group 10 element is Pt, the inorganic support comprises 3 wt% to 65 wt% of a Group 2 element based on the mass of the inorganic support, the Group 2 element is Mg, at least a portion of the inorganic support is MgO or a mixed oxide containing MgO, and the at least partially deactivated catalyst further comprises 0.1 wt% to 5 wt% of an accelerator based on the mass of the inorganic support, the accelerator being the following elements: Sn, Ag, Cu, It is one or more of those combinations or mixtures, and The aforementioned process, (I) A heated gas mixture having a concentration of more than 5 mol% based on its total moles. 2 A step of generating a precursor catalyst by heating the at least partially deactivated catalyst using a heated gas mixture containing O, (II) Oxidizing gases, where H is present in a quantity of 5 mol% or less based on the total moles. 2 The steps include supplying an oxidizing gas containing O, (III) A step of generating an oxidation precursor catalyst by contacting the precursor catalyst with the oxidizing gas at an oxidation temperature in the range of 620°C to 1,000°C for a duration of at least 30 seconds, (IV) A step of obtaining a regenerated catalyst from the oxidation precursor catalyst. The process including the process described above.

2. The process according to claim 1, wherein the inorganic support is (a) MgO, (b) MgO-Al₂O₃ mixed metal oxide, or (c) MgAl₂O₄, and (b) and (c) have a mass ratio of Mg to Al of 0.05 to 6.

3. The process according to claim 1, wherein the at least partially deactivated catalyst further comprises up to 5 wt% of an alkali metal element disposed on the inorganic support, the alkali metal element comprising at least one of Li, Na, K, Rb, and Cs.

4. The regenerating catalyst is one or more C 2 -C 16 Straight-chain or branched alkanes, or one or more carbon atoms. 4 -C 16 Cyclic alkanes, one or more C 8 -C 16 The process according to claim 1, having the ability to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of a hydrocarbon-containing feed comprising alkyl aromatic hydrocarbons or mixtures thereof, wherein the active component of the regenerating catalyst comprises a Group 10 element.

5. Step (II) is (IIa) The step of supplying the oxidizing gas at a temperature below the oxidation temperature, (IIb) The step of preheating the oxidizing gas to a temperature higher than the temperature of the precursor catalyst before contact in step (III). The process according to claim 1, including the process described in claim 1.

6. moreover, (V) Step (III) includes a step of heating the oxidizing gas, the precursor catalyst, or both by using a radiant / conductive heat source, a heat exchanger, or a combination thereof, The process according to claim 1.

7. Step (IV) is (IVa) contacting the pre-oxidation precursor catalyst with a first stripping gas that does not contain O 2 to produce a stripped pre-oxidation precursor catalyst; (IVb) A step of obtaining the regenerated catalyst from the exfoliated oxidation precursor catalyst, The process according to claim 1, including the process described in claim 1.

8. Step (IV) is (IVc) The oxidation precursor catalyst or the exfoliation oxidation precursor catalyst is H 2 A step of generating a reduction catalyst by contacting it with the contained atmosphere, (IVd) A step of obtaining the regenerating catalyst from the reduction catalyst. The process according to claim 7, including the process described in claim 7.

9. Step (IVd) is (IVd-1) A step of generating the regenerated catalyst by contacting the reduction catalyst with a second stripping gas. The process according to claim 8, including the process described in claim 8.

10. Step (IVc) is performed at a temperature of the oxidation precursor catalyst that is higher than the operating temperature of the regenerated catalyst, and step (IVd) is further performed. (IVd-2) A step of cooling the reduction catalyst or the regeneration catalyst to the operating temperature for a duration of 10 minutes or less, 5 minutes or less, 1 minute or less, 30 seconds or less, 10 seconds or less, 5 seconds or less, 1 second or less, 0.5 seconds or less, 0.1 seconds or less, 0.01 seconds or less, or 0.001 seconds or less. The process according to claim 8, including the process described in claim 8.

11. A dehydrogenation process using the regenerating catalyst produced by the process described in any one of claims 1 to 10, (VI) Contacting a hydrocarbon-containing feed with the regenerating catalyst to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of at least a portion of the hydrocarbon-containing feed to produce the at least partially deactivated catalyst comprising the Group 10 elements, the inorganic support, and the impurities, and an effluent comprising one or more upgraded hydrocarbons and molecular hydrogen, wherein the hydrocarbon-containing feed comprises one or more C 2 -C 16 Straight-chain or branched alkanes, one or more types of carbon 4 -C 16 Cyclic alkanes, one or more C 8 -C 16 A step comprising alkyl aromatic hydrocarbons or a mixture thereof, (VII) A step in which steps (I) to (IV) are repeated, wherein an additional oxidation precursor catalyst is generated in step (III), and an additional regenerating catalyst is obtained from the additional oxidation precursor catalyst in step (IV), (VIII) The step of contacting an additional amount of the hydrocarbon-containing feed with at least a portion of the additional regenerating catalyst to generate an additional at least partially deactivated catalyst and an additional effluent. The dehydrogenation process, including the dehydrogenation process.

12. The dehydrogenation process according to claim 11, wherein the cycle time from the contact of the hydrocarbon-containing feed with the regenerating catalyst in step (VI) to the contact of the additional amount of hydrocarbon-containing feed with the additional regenerating catalyst in step (VIII) is 5 hours or less.

13. A hydrocarbon upgrade process, (I) A step of contacting a hydrocarbon-containing feed with a catalyst comprising a Group 10 element and an inorganic support to cause one or more dehydrogenation, dehydrogenation aromatization, and dehydrogenation cyclization of at least a portion of the hydrocarbon-containing feed to produce at least a partially deactivated catalyst comprising the Group 10 element, the inorganic support, and impurities, and an effluent comprising one or more upgraded hydrocarbons and molecular hydrogen, The hydrocarbon-containing feed contains one or more C 2 -C 16 Straight-chain or branched alkanes, or one or more carbon atoms. 4 -C 16 Cyclic alkanes, one or more C 8 -C 16 Containing alkyl aromatic hydrocarbons or mixtures thereof, The group 10 element has a concentration in the range of 0.01 wt% to 1 wt% based on the mass of the inorganic support, and the group 10 element is Pt. The inorganic support contains 3 wt% to 65 wt% of a group 2 element based on the mass of the inorganic support, the group 2 element being Mg, and at least a portion of the inorganic support is MgO or a mixed oxide containing MgO. The at least partially deactivated catalyst further comprises 0.1 wt% to 5 wt% of an accelerator based on the mass of the inorganic support, wherein the accelerator is composed of the following elements: Sn, Ag, Cu, It is one or more of those combinations or mixtures. The hydrocarbon-containing feed and the catalyst are in contact at a temperature in the range of 300°C to 900°C, and The step includes the provision that the one or more upgraded hydrocarbons include at least one of dehydrogenated hydrocarbons, dehydrogenated aromatic hydrocarbons, and dehydrogenated cyclized hydrocarbons, (II) A heated gas mixture having a concentration of more than 5 mol% based on its total moles. 2 A step of generating a precursor catalyst by heating the at least partially deactivated catalyst using a heating gas mixture containing O, (III) Oxidizing gases, where H is present in a total mole amount of 2 mol% or less. 2 The steps include supplying an oxidizing gas containing O, (IV) A step of generating an oxidation precursor catalyst by contacting the precursor catalyst with the oxidizing gas at an oxidation temperature in the range of 620°C to 1,000°C for a duration of at least 30 seconds, (V) A step of obtaining a regenerated catalyst from the oxidation precursor catalyst, (VI) The step of contacting an additional amount of the hydrocarbon-containing feed with at least a portion of the regenerated catalyst to generate an additional at least partially deactivated catalyst and additional effluent. The process including the process described above.

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