US20220048019A1

US20220048019A1 - Methods and reforming systems for re-dispersing platinum on reforming catalyst

Info

Publication number: US20220048019A1
Application number: US17/512,792
Authority: US
Inventors: David J. Zalewski; Vidya Dharmagadda
Original assignee: Marathon Petroleum Co LP
Current assignee: Marathon Petroleum Co LP
Priority date: 2019-05-09
Filing date: 2021-10-28
Publication date: 2022-02-17
Also published as: US20200353456A1; CA3199701A1; CA3080518A1; CA3080518C

Abstract

Methods and systems for re-dispersing platinum on catalysts used in continuous catalyst regeneration reformer systems are disclosed. Some aspects of the disclosure provide, for example, methods of evaluating the platinum re-dispersion of a reforming catalyst in a small-scale reactor for use in a continuous catalyst regeneration reformer system and methods of improving the activity and selectivity of reforming catalysts for use in a continuous catalyst regeneration reformer system by selection of appropriate reaction parameters in a small-scale reactor for use in a continuous catalyst regeneration reformer system.

Description

CROSS-REFERENCE TO RELATED APPLICATIONS

This is a divisional of U.S. Non-Provisional application Ser. No. 16/869,186, filed May 7, 2020, titled “METHODS AND REFORMING SYSTEMS FOR RE-DISPERSING PLATINUM ON REFORMING CATALYST,” which claims priority to and the benefit of U.S. Provisional Application No. 62/845,485, filed May 9, 2019, titled “RE-DISPERSING PLATINUM ON REFORMING CATALYST,” the disclosures of which are incorporated herein by reference in their entirety.

FIELD OF THE DISCLOSURE

The disclosure herein relates to methods and systems for evaluating or controlling the platinum re-dispersion on reforming catalysts used in a continuous catalyst regeneration (CCR) reformer system.

BACKGROUND

Catalytic processes for the conversion of hydrocarbons using platinum group metals and a catalyst support are well known and extensively used. For example, metal-containing reforming catalysts can be used in continuous catalyst regeneration (CCR) reforming processes as understood by those skilled in the art, and such catalysts are commonly referred to as CCR reforming catalysts. CCR reforming processes may generally be referred to as “catalytic reforming” processes. One CCR reforming process is the catalytic reforming of naphtha. In such a process, the naphtha is co-processed with hydrogen over platinum-containing reforming catalysts, for example, as described in more detail in U.S. Pat. No. 8,778,823 to Youkan et al. During naphtha (and other types of) reforming, the catalyst becomes deactivated, attributed at least in part to the accumulation of coke deposits. Reconditioning of the catalyst to remove coke deposits is necessary to restore the activity of the catalyst. Coke is normally removed from deactivated catalyst by contacting the coke-containing catalyst at high temperature with an oxygen-containing gas to combust and to essentially convert the coke to carbon dioxide and water in a regeneration process. Cycling the catalyst particles between the reducing conditions of the reactor and the oxidizing conditions of the regenerator can lead to platinum agglomeration and can degrade catalyst activity.
In a commercial setting, CCR reforming processes are commonly conducted within an integrated processing unit which contains equipment, catalyst(s), sorbent(s) and chemical(s) used in the reaction. The equipment can include, e.g., reactors, reactor internals for distributing feed and containing catalyst, other vessels, heaters, heat exchangers, conduits, valves, pumps, compressors and associated components known to those of skilled in the art. For example, a catalytic-reforming system may have various sections, including a reaction section (wherein the desired reaction occurs, catalyzed by the CCR reforming catalyst) and a regeneration section (wherein spent CCR reforming catalyst is regenerated). The regeneration section typically includes various zones, including, e.g., a burn zone, a halogenation zone, and a drying zone. Typically, these separate zones are contained within a single regeneration vessel and may be in serial progression, for example. Equipment and technology for continuously or semi-continuously removing catalyst particles from reaction sections and for coke removal in regeneration sections of such systems are generally known.
In order to combust coke buildup on catalyst particles, such spent catalyst particles are generally passed from the reaction section into the regeneration section. A regeneration gas, having a low concentration of oxygen, is continuously circulated within the regeneration section. The first zone of the regeneration section, into which the particles are passed, is a burn zone wherein coke combustion is carefully controlled by limiting the oxygen concentration. From the burn zone, a flue gas containing oxygen, water, and the byproducts of coke combustion is continually withdrawn. Coke combustion is controlled by contacting the coke-containing catalyst particles passing through the regeneration section with the regeneration gas that is continuously recirculated within the regeneration section. The controlled burn limits the temperature exotherm experienced by the catalyst. A small stream of combustion gas is added to the regeneration gas so as to replace the oxygen consumed in the combustion of coke and a small amount of the flue gas is vented off from the regeneration gas to allow for the addition of the combustion gas. The addition of combustion gas and the venting of flue gas establish a steady state condition that produces a nearly constant average concentration of water and oxygen in the regeneration gas. Despite the controlled conditions, platinum atoms slowly agglomerate and a re-dispersion step is necessary.
After the burn zone, the spent metal-containing catalyst particles are passed to a halogenation zone. In this zone, chlorine and/or another halogen circulates through the zone in a halogenation loop. Spent catalyst that has passed through the burn zone as referenced above commonly exhibit platinum agglomeration. Platinum agglomeration is a major factor contributing to poor performance of commercial CCR catalyst and may affect the activity, selectivity, and stability of reforming catalysts. To renew the reforming activity, therefore, the coke-free catalyst exiting the burn zone is passed to the halogenation zone where the platinum atoms are re-dispersed on the reforming catalyst. The halogenation zone of the regeneration section is designed to control halogen levels, oxygen levels, moisture content, and temperature to re-disperse the platinum (or other metal) associated with the catalyst. Contacting the catalyst with the halogenation gas re-disperses platinum group metals on the catalyst particles and adds some halogen to replace halogen lost from the catalyst during naphtha processing. The halogen gas added to the halogenation loop may enter the loop in admixture with air or other oxygen-containing gas. The process that occurs in the halogenation zone re-disperses the platinum group metals on the catalyst and is referred to as “white burn” when employed after the regenerator burn zone, as described previously.
From the halogenation zone, the catalyst particles are passed into a drying zone. A heated gas contacts the catalyst particles and drives moisture from the particles. Typically, the heated gas is air or an oxygen-containing gas that is introduced to the drying zone as the drying medium and passes upward through the halogenation zone to the burn zone to also provide the combustion gas therein. Following the drying zone, regenerated catalysts particles are cycled back to the reaction section to complete the continuous flow through the reaction and regeneration sections.
Conditions for such regeneration processes (and, in particular, conditions in the halogenation zone of the regenerator section) have not been extensively studied to allow for testing and/or evaluation of various reforming catalysts (e.g., commercially available catalysts) and/or various process conditions prior to commercial use.

SUMMARY OF THE DISCLOSURE

Applicant has recognized that it would be advantageous to develop methods and systems for evaluating the platinum re-dispersion of various CCR catalysts in CCR reformer systems, controlling and/or simulating the oxychlorination conditions present in commercial halogenation zones in small-scale reactors, easily comparing the re-dispersion of various commercial catalysts, and improving the selectivity and activity of such catalysts via selection of appropriate regeneration conditions.
Accordingly, the disclosure herein provides one or more embodiments of methods of evaluating platinum re-dispersion in the context of reformer operation. The disclosure also provides one or more embodiments of methods of controlling platinum re-dispersion in the context of reformer operation. In some embodiments, the disclosure provides a method of evaluating the characteristics of various reforming catalysts used in CCR reformer systems. Such processes and methods advantageously provide for the control of one or more oxychlorination conditions (e.g., catalyst chloride level, time, temperature, and/or oxygen level) in a small-scale reactor. This may occur, for example, by providing the ability to directly compare the re-dispersion of different CCR catalysts under varying conditions and reaction atmospheres. The parameters of these methods may be controlled or adjusted, for example, to improve the activity or selectivity of the reforming catalysts used therein. In some embodiments, such parameters may then be applied on a larger scale, e.g., to provide enhanced reaction efficiency.
Some aspects of the disclosure provide methods of evaluating the platinum re-dispersion of a reforming catalyst in a small-scale reactor for use in a continuous regeneration system for a reforming process. The small, lab-scale re-dispersion process can be used to identify or rule out problems with the commercial regenerator. For example, a poorly dispersed catalyst sample can be subjected to the small-scale re-dispersion process; if the platinum dispersion is restored in the small-scale re-dispersion process, the commercial regeneration conditions can be adjusted accordingly, or if the platinum dispersion is not restored in the small-scale re-dispersion process, this may indicate that the catalyst has been poisoned.
Another aspect of the disclosure provides methods of evaluating platinum re-dispersion of a reforming catalyst in a small-scale reactor for use in a CCR reformer system (e.g., prior to implementation on a larger scale). For example, such methods may comprise providing an agglomerated reforming catalyst, subjecting the agglomerated reforming catalyst to one or more oxychlorination conditions to provide a re-dispersed reforming catalyst, wherein the subjecting step is configured to simulate a halogenation zone in a continuous catalyst regeneration reformer system, and controlling the one or more oxychlorination conditions to evaluate platinum dispersion on the re-dispersed reforming catalyst. The oxychlorination conditions may be selected from the group consisting of a time, a temperature, a catalyst chloride level, and an oxygen level, for example. In some embodiments, the method additionally may include measuring the platinum dispersion on the re-dispersed reforming catalyst.
In some embodiments, the step of subjecting the agglomerated reforming catalyst may be at least partially conducted in a small-scale reactor to simulate a halogenation zone in a continuous catalyst regeneration reformer system. For example, in some embodiments, the agglomerated reforming catalyst may be subjected to each of the oxychlorination conditions in the small-scale reactor. In such embodiments, one or more, or all, of the oxychlorination conditions may be controlled in the small-scale reactor. In other embodiments, the agglomerated reforming catalyst may be treated with a chloride source as a part of the subjecting step, and subsequently the agglomerated reforming catalyst may be loaded into the small-scale reactor. In such embodiments, the agglomerated reforming catalyst may be loaded into the small-scale reactor and then subjected to the remaining oxychlorination conditions while in the small scale reactor.
In some embodiments, such methods may further comprise subjecting a reforming catalyst to a steam deactivation process to provide the agglomerated reforming catalyst in the first method step. In some embodiments, such methods further may comprise adjusting the one or more oxychlorination conditions to provide a re-dispersed reforming catalyst with higher platinum dispersion. In some embodiments, the one or more oxychlorination conditions may be adjusted to provide a re-dispersed reforming catalyst with one or both of a higher activity and a higher selectivity. In some embodiments, the one or more oxychlorination conditions may be adjusted to provide a re-dispersed reforming catalyst capable of producing a higher unit yield. In some embodiments, the agglomerated reforming catalyst may be in particulate form and comprises a platinum component and a halogen component on a porous carrier. In some embodiments, the halogen component may be chlorine. In some embodiments, the agglomerated reforming catalyst further may comprise a promoter or a stabilizer.
Some embodiments of the disclosure also provide methods of improving the platinum dispersion on a re-dispersed reforming catalyst by adjusting the catalyst chloride level to a level of about 0.5 to about 1.5 wt. % Cl. In some embodiments, the platinum dispersion on a re-dispersed reforming catalyst may be improved by adjusting the catalyst chloride level to a level of about 1.0 wt. % Cl or higher. In some embodiments, the platinum dispersion on a re-dispersed refining catalyst may be improved by adjusting the temperature in the small-scale reactor to a temperature of about 400° C. to about 600° C. In some embodiments, the platinum dispersion on a re-dispersed reforming catalyst may be improved by adjusting the oxygen content in the small-scale reactor to a value of about 5% to about 30%. In some embodiments, the platinum dispersion on a re-dispersed reforming catalyst may be improved by adjusting the time in the small-scale reactor to a value of about 1 hour to about 4 hours. In further embodiments, the method may include evaluating two or more sets of oxychlorination conditions. The method also may include selecting the set of oxychlorination conditions associated with the highest catalyst platinum dispersion for use on a CCR reformer system and, optionally, implementing such set of oxychlorination conditions within the CCR reformer system.
Other aspects of the disclosure may provide a method of selecting a re-dispersed reforming catalyst for use in a CCR reformer system. For example, such selecting may comprise performing one or more of the methods disclosed herein on two or more different agglomerated reforming catalysts and selecting the re-dispersed reforming catalyst demonstrating the highest platinum dispersion for use within a CCR reformer system. The method may, in some embodiments, further comprise implementing the selected re-dispersed reforming catalyst in a CCR reformer system for reforming. In some embodiments, at least one of the agglomerated reforming catalysts evaluated may comprise a promoter and/or a stabilizer.
In yet other embodiments, methods of operating a CCR reformer system for reforming are disclosed, wherein a regeneration section includes a burn zone, a halogenation zone, and a drying zone in serial progression. In some embodiments, the method may include transfer of catalyst particles, containing a platinum group metal and having coke deposited thereon, to the burn zone and contacting the catalyst particles with an oxygen-containing regeneration gas to combust coke from the particles, passing catalyst particles from the burn zone to halogenation zone, contacting the catalyst particles with a halogen-containing gas in the halogenation zone, re-dispersing the platinum group metal on the catalyst particles, continuously circulating the halogen-containing gas from halogenation gas outlet to a halogenation gas inlet in the halogenation zone, maintaining a halogen concentration on the surface of the catalyst particles of at least about 1.0 weight percent in the halogenation zone, passing catalyst particles from the halogenation zone to a drying zone, and contacting the catalyst particles with a drying gas in the drying zone. In some embodiments, the halogen concentration on the surface of the catalyst particles in the halogenation zone is maintained above 1.2 weight percent. In some embodiments, the halogen concentration on the surface of the catalyst particles in the halogenation zone is maintained in the range of about 1.0 weight percent to about 1.5 weight percent.
The disclosure includes any combination of two, three, four, or more features or elements set forth in this disclosure or recited in any one or more of the claims, regardless of whether such features or elements are expressly combined or otherwise recited in a specific embodiment description or claim herein. This disclosure is intended to be read holistically such that any separable features or elements of the disclosure, in any of its aspects and embodiments, should be viewed as intended to be combinable, unless the context of the disclosure clearly dictates otherwise.

BRIEF DESCRIPTION OF THE DRAWINGS

Having thus described the disclosure in general terms, reference will now be made to the accompanying drawings, which are not necessarily drawn to scale, and wherein:

FIG. 1 illustrates a method of evaluating the platinum re-dispersion of a reforming catalyst in a small-scale reactor for use in a CCR reformer system for reforming, according to an embodiment of the disclosure;

FIG. 2 illustrates a large-scale CCR reformer system for reforming, according to an embodiment of the disclosure.

DETAILED DESCRIPTION OF THE DISCLOSURE

The disclosure now will be described more fully hereinafter with reference to specific embodiments and particularly to the various drawings provided herewith. Indeed, the disclosure may be embodied in many different forms and should not be construed as limited to the embodiments set forth herein; rather, these embodiments are provided so that this disclosure will satisfy applicable legal requirements. As used in the specification, and in the appended claims, the singular forms “a,” “an,” “the,” include plural referents unless the context clearly dictates otherwise.
The disclosure generally provides methods for re-dispersing platinum atoms on reforming catalysts used in a CCR reformer system as will be understood by one skilled in the art. In particular, and provided in further detail herein below, the disclosure includes embodiments of methods of evaluating platinum re-dispersion of reforming catalysts that have been re-dispersed in a small-scale reactor by controlling key oxychlorination conditions or parameters (e.g., the catalyst chloride level, temperature, time, and oxygen level) to simulate a halogenation zone, e.g., such as would be understood by those skilled in the art to be used in commercial CCR reforming processes/within a large-scale CCR reformer system. It should be noted that such methods of evaluating the reforming catalyst do not require the typical reaction section and regeneration section (e.g., as would be present in a commercial CCR unit). Instead, an already agglomerated reforming catalyst (e.g., that has been used in a commercial CCR unit previously) or a reforming catalyst that has been steam deactivated to create platinum agglomeration (e.g., to simulate the aging effects of using the catalyst in a commercial CCR unit) is subjected to one or more oxychlorination conditions at least partially in a small-scale reactor to simulate the halogenation zone. Generally, a “small-scale reactor” as described herein, refers to any reactor vessel that is small enough to be used in a laboratory setting and which allows for control and/or adjustment of the one or more oxychlorination conditions therein. In some embodiments, the small-scale reactor may contain about 1 to about 1,000 grams of reforming catalyst, or about 2.5 to about 500 grams of reforming catalyst, or about 5 to about 100 grams of reforming catalyst. In some embodiments, a micro-reactor may be used. For example, certain micro-reactor technology uses devices with dimensions in the sub-millimeter range to perform chemical transformations. These micro-reactor systems may, in some embodiments, be designed to take advantage of micro-flow phenomena, which enhances mass and heat transfer properties due to the high area-to-volume ratios.
Advantageously, such methods may provide comparative re-dispersion data of different reforming catalysts under controlled conditions (e.g., allowing the user to determine the best catalyst of those tested for implementation in the large scale CCR reformer system), and the conditions may be adjusted so as to predict improvement in the selectivity, activity, and stability of an individual catalyst on a larger scale (such that these conditions may subsequently be implemented on the large-scale CCR reformer system when using such catalyst). As noted above, such small-scale evaluation and control of these oxychlorination conditions, and their effect on the platinum re-dispersion of various catalysts and CCR reforming systems, has not been previously achieved in the industry.
In addition, the methods provided herein can be used to identify or rule out problems with the commercial CCR reformer systems. For example, commercial reforming catalysts that are currently in use may be evaluated using the methods provided herein to troubleshoot issues with inefficient reforming systems. In such embodiments, a catalyst sample exhibiting poor performance on a commercial CCR unit can be subjected to the small-scale re-dispersion processes described herein to determine the cause of the poor performance. For example, if the platinum dispersion is restored on the commercial catalyst in the small-scale re-dispersion processes described herein, this indicates that the commercial regeneration conditions being used in the commercial CCR unit are inefficient and can be adjusted accordingly, or if the platinum dispersion is not restored on the commercial catalyst in the small-scale re-dispersion process, this may indicate that the catalyst has been poisoned and is no longer suitable for use in CCR reformer systems.
Catalysts used for reforming reactions (“reforming catalysts” and/or “catalyst systems” and/or “catalysts” as referred to herein) are comprised of one or more metals and a halogen supported on a porous carrier. Generally, the “one or more metals” may be a Group VIII noble metal, e.g., such as platinum, iridium, rhodium, palladium, and the like. The particular metal or combinations of metals present in the reforming catalyst may vary; however, typically the reforming catalyst contains at least some amount of platinum. A “halogen” as used herein, refers to a Group XVII halogen or halogen-containing component, e.g., such as fluorine, chlorine, bromine, iodine, and astatine. The particular halogen used may vary; however, typically the halogen is a chloride containing compound. A “porous carrier” as used herein, refers to a refractory metal inorganic oxide, e.g., such as alumina, silica, silica-alumina, and the like. The particular refractory metal inorganic oxide forming the porous carrier may vary; however, typically the porous carrier is an alumina support.
In some embodiments, the catalysts used herein may be referred to as a “multi-metallic catalyst system”, e.g., such as bi-metallic catalyst systems, tri-metallic catalyst systems, and the like. Generally, “multi-metallic catalyst systems” as used herein, refer to reforming catalysts that comprise a porous carrier having two or more metallic components supported thereon. In some embodiments, a reforming catalyst further may have a promoter and/or a stabilizer supported thereon. For example, a “promoter” may refer to a substance added to a reforming catalyst to improve its performance in a chemical reaction. By itself, the substance may have little or no catalytic effect. Such promoters may comprise one or more metallic ions that are supported on the catalyst system. In some embodiments, adding a promoter metal to the reforming catalyst, for example, may result in better yield, but such advantages may be offset by making it more difficult to maintain high platinum (Pt) dispersion in the reforming catalyst.
Catalyst vendors in the industry continually work to improve the efficiency and other characteristics of reforming catalysts. Such improvements may be achieved by creating new catalyst systems or adding different promoters or stabilizers to already known catalysts. Catalysts and catalyst systems may be referred to herein as “old generation” or “new generation catalysts”; each referring to how recently the catalyst was discovered/developed. For example, old generation catalysts typically refer to catalysts that have been commercially available and used in commercial CCR units historically for many years as would be understood by those skilled in the art, whereas new generation catalysts typically refer to catalysts that are relatively new developments that may or may not have been used in commercial CCR units previously. The effectiveness of a particular catalyst, however, does not necessarily correlate to the particular generation of that catalyst. For example, in some embodiments, newer generation catalysts may not be as effective as older generation catalysts, and in other embodiments, the newer generation catalysts may perform better. Generally, the performance of the catalyst or catalyst system can be evaluated by a number of factors, e.g., such as the platinum dispersion on the surface of the reforming catalyst, the selectivity of the reforming catalyst, the activity of the reforming catalyst, and the like. Thus, a reforming catalyst exhibiting better performance may have a higher platinum dispersion thereon and/or higher selectivity and/or higher activity than a comparable catalyst, whereas a catalyst exhibiting lesser performance may have a lower platinum dispersion thereon and/or lower selectivity and/or lower activity.
Generally, the catalyst is provided in particulate form, and such particles may vary in size and/or shape. Since CCR units circulate catalyst from the reaction section to the regeneration section, they may be cylindrical or spheroidal in shape with diameters from about 1/16^thto about ⅛^thinch (1.5-3.1 mm) in size. One or more of the methods and systems described herein may also applicable for evaluating fixed bed reforming catalysts. Fixed bed reforming catalysts may be in the form of an extrudated material having a diameter of from about 1/16^thto about ⅛^thinch (1.5-3.1 mm), though they may be as large as ¼ inch (6.35 mm) in diameter. It should be noted that any type of reforming catalyst generally suitable for use in commercial CCR processes generally is meant to be suitable for use in the methods described more specifically herein.
As depicted in FIG. 1, one embodiment of the disclosure provides a method of evaluating the platinum re-dispersion on a reforming catalyst in a small-scale reactor for use in a CCR reformer system (e.g., a large scale system). Such methods may comprise, for example, the steps of: (i) providing an agglomerated reforming catalyst (e.g., as shown at operation 2); (ii) subjecting the agglomerated reforming catalyst to one or more oxychlorination conditions at least partially in a small-scale reactor to provide a re-dispersed reforming catalyst, wherein the subjecting step is configured to simulate a halogenation zone in a continuous catalyst regeneration reformer system (e.g., as shown at operation 4); and (iii) controlling the one or more oxychlorination conditions to evaluate platinum dispersion on the re-dispersed reforming catalyst. The oxychlorination conditions, for example, may be selected from the group consisting of a time, a temperature, a catalyst chloride level, and an oxygen level (e.g., as shown at operation 6). The method also may include measuring the platinum dispersion on the re-dispersed reforming catalyst (e.g., as shown at operation 8).
Applicant advantageously has discovered that repeatable platinum dispersion values may be obtained by controlling key parameters during a simulated re-dispersion process in a small-scale reactor, e.g., by controlling one or more oxychlorination conditions in the small-scale reactor according to embodiments of methods provided herein. Thus, under controlled oxychlorination conditions in a small-scale reactor, the platinum re-dispersion on individual reforming catalysts may be measured, evaluated, adjusted, and/or compared to the platinum re-dispersion exhibited on other reforming catalysts. Generally, it is desirable to understand how platinum dispersion will be maintained throughout the life of the reforming catalyst during use in a commercial CCR unit. Using the methods described herein, it should be noted that the platinum re-dispersion of various reforming catalyst samples can advantageously be evaluated before being loaded into a commercial CCR unit.
The terms “platinum re-dispersion” and “platinum dispersion” may be used interchangeably herein, and generally refer to the dispersion and/or distribution of platinum atoms on the surface of the reforming catalyst after the reforming catalyst has been subjected to the one or more oxychlorination conditions to re-disperse the platinum thereon. The dispersion of platinum atoms on the surface of the reforming catalyst is measured as a percentage, wherein the “platinum dispersion percentage” is equal to the number of active platinum sites (e.g., availability to catalytic reactions and/or providing at least some catalytic reactivity) divided by the total amount of platinum present on the reforming catalyst. Generally, it should be noted that lower platinum dispersion percentages indicate uneven distribution and/or some degree of agglomeration of platinum atoms on the surface of the reforming catalyst, whereas higher platinum dispersion percentages indicate more even distribution and/or minimal to no agglomeration of platinum atoms on the surface of the reforming catalyst. For example, a 100% platinum dispersion value can indicate that the platinum atoms are substantially evenly distributed on the surface of the reforming catalyst, such that all platinum atoms provide active reaction sites. In some embodiments, the platinum re-dispersion on the catalyst may be measured using chemisorption techniques to compare platinum dispersion values before and after the lab re-dispersion process. Other techniques, such as scanning electron microscopy (SEM) and/or x-ray diffraction analyses can be used to monitor platinum dispersion and clustering, for example. Generally, re-dispersed catalyst samples are removed from the small-scale reactor prior to measurement of the platinum dispersion.
In addition, the effect of a promoter or a stabilizer added to a catalyst system may be evaluated to determine the effect of the added promoter or stabilizer on the overall re-dispersion on the reforming catalyst when subjected to oxychlorination conditions. Advantageously, such methods also allow for efficient testing of the platinum re-dispersion of multiple, different reforming catalysts on a small-scale prior to using such catalysts on large-scale, e.g., such as commercially available CCR reforming processes. It should be noted that catalysts showing a low platinum re-dispersion when evaluated according to the methods provided herein may struggle to maintain high platinum dispersion values in a commercial CCR unit, which may translate into lower reforming activity of the overall CCR unit. Meanwhile, catalysts showing high platinum re-dispersion when evaluated according to the methods provided herein advantageously may maintain high platinum dispersion values in a commercial CCR unit, which may translate into higher reforming activity, higher catalyst selectivity, and improved yield.
As noted above, the methods and systems described herein require providing an agglomerated reforming catalyst, e.g., as noted at operation 2. Generally, a deactivation process is used to provide an agglomerated reforming catalyst. During the deactivation process, chlorides are stripped from the catalyst and the platinum atoms (or other metals) contained thereon are agglomerated. In some embodiments, for example, steam deactivation processes are used to artificially age the catalyst samples to provide an agglomerated catalyst sample. The steam deactivation process reduces the catalyst surface and mimics the aging that occurs in a commercial CCR unit. The particular processes used for deactivating the catalyst samples to simulate aging (and agglomerate the platinum atoms) and/or the conditions used during such processes may generally vary. For example, the agglomerated catalyst samples may be obtained directly from a commercial CCR unit (e.g., such that artificial aging of the catalyst is not necessary), or a lab agglomerated catalyst (e.g., that has been steam deactivated to simulate aging of the catalyst) may be used. When preparing a lab agglomerated catalyst, it should be noted that, by controlling the steam deactivation process conditions (e.g., such as temperature, time, and percent steam), the aging process can mimic 1-10 years of operation in a commercial CCR unit. For example, a lab agglomerated catalyst sample can be generated by treating the reforming catalyst with steam using temperatures between about 1000° F. and about 1300° F. In some embodiments, the reforming catalyst may be treated with steam using a temperature of at least about 1000° F., at least about 1050° F., at least about 1100° F., at least about 1150° F., at least about 1200° F., at least about 1250° F., at least about 1300° F., or higher.
After providing the agglomerated reforming catalyst, it is subjected to one or more oxychlorination conditions at least partially in a small-scale reactor to simulate the halogenation zone in a commercial CCR unit. As noted above, for example, the methods and systems described herein allow for control of one or more oxychlorination conditions, optionally in the small-scale reactor, to determine the effect of those particular conditions on the platinum dispersion on a re-dispersed reforming catalyst. In particular, the catalyst chloride level in the reactor, the temperature in the reactor, the oxygen level in the reactor, and the time of the reaction may be controlled to determine the difference in platinum dispersion between multiple reforming catalysts at various conditions (e.g., which reforming catalyst performs best using set conditions) and may be controlled to determine which combinations of conditions provide the desired re-dispersion for a particular reforming catalyst (e.g., which conditions provide the best platinum dispersion for a particular catalyst).
In some embodiments, the platinum re-dispersion on a reforming catalyst may be improved by controlling the halide (e.g., chloride) level on the catalyst surface before and/or during its residence within the small-scale reactor during the re-dispersion process. “Catalyst chloride level” as used herein, refers to the chloride level on the surface of the reforming catalyst and is typically measured when the catalyst is removed from the small-scale reactor, after being subjected to the one or more oxychlorination conditions during the re-dispersion process. Generally, the amount of chloride ions on the catalysts surface can be controlled to maintain peak activity of the reforming catalyst. Advantageously, the presence of chloride ions in the reforming catalyst may help maintain a high platinum dispersion during processing, for example, because the chloride ions react with the oxidized platinum ions which helps redistribute platinum over the catalyst support. In addition, the chloride ions may interact with the porous carrier (e.g., alumina support) to create the acidity needed for reforming reactions.
It should be noted that reforming catalysts are typically pre-chlorided prior to use in commercial CCR units. However, some of this chloride is lost during the reaction in the reaction section and in the burn zone of the regeneration section, reducing the chloride content below desired levels. Thus, subjecting the reforming catalysts to a chloride-containing gas, for example, in the halogenation zone of a commercial regeneration process, allows the lost chloride to be replenished on the reforming catalyst. Generally, the chloride component in commercial CCR units may be injected or sprayed into the halogenation zone. For example, the chloride component in commercial units may include an organic chloride, e.g., such as perchloroethane. However, in the processes and methods described herein, the agglomerated reforming catalyst is treated with a chloride source (e.g., such as hydrochloric acid (“HCl”)) and subsequently the agglomerated reforming catalyst is loaded into the small-scale reactor to impart the desired catalyst chloride level on the reforming catalyst while in the small-scale reactor. Generally, addition of this chloride source prior to loading the agglomerated reforming catalyst into the small-scale reactor can create the effect of re-chloriding the agglomerated reforming catalyst, such as would occur when the catalyst comes into contact with the halogen-containing gas in the halogenation zone of a commercial CCR unit. The amount of HCl treated onto the agglomerated reforming catalyst may vary and typically HCl is treated onto the agglomerated reforming catalyst in an amount sufficient to provide the desired catalyst chloride level in the small-scale reactor. For example, the catalyst chloride level may be adjusted to be in the range of about 0.5 to about 1.5 weight percent Cl, about 0.7 to about 1.3 weight percent Cl, or about 1.0 to about 1.2 weight percent Cl. In some embodiments, the catalyst chloride level may be maintained at above 0.7 weight percent Cl, above 1.0 weight percent Cl, above 1.2 weight percent Cl, or above 1.3 weight percent Cl. In particular embodiments, the catalyst chloride level is about 1.0 weight percent Cl or greater. In some embodiments, the moisture content and/or the temperature within the small-scale reactor may also influence the catalyst chloride level.
In some embodiments, the platinum re-dispersion of the reforming catalyst may be improved by controlling the temperature in the small-scale reactor during the re-dispersion process. For example, the temperature in the small-scale reactor may be adjusted to be in the range of about 400° C. to about 600° C., about 450° C. to about 575° C., or about 500° C. to about 550° C. In some embodiments, the temperature in the small-scale reactor may be adjusted to be above about 450° C., above about 475° C., above about 500° C., above about 525° C., above about 550° C., or higher. In some embodiments, the temperature in the small-scale reactor may be adjusted to be about 400° C. or greater, about 450° C. or greater, about 475° C. or greater, about 500° C. or greater, about 525° C. or greater, or about 550° C. or greater.
In some embodiments, the platinum re-dispersion of the reforming catalyst may be improved by controlling the oxygen content in the small-scale reactor during the re-dispersion process. For example, the oxygen content in the small-scale reactor may be adjusted to be in the range of about 5% to about 50% oxygen, about 10% to about 30%, or about 20% to about 25%. In some embodiments, the oxygen content in the small-scale reactor may be adjusted to be above about 10%, above about 15%, above about 20%, above about 25%, above about 30%, and higher. In some embodiments, the oxygen content in the small-scale reactor may be adjusted to be about 5% or greater, 10% or greater, 15% or greater, 20% or greater, 25% or greater, or 30% or greater.
In some embodiments, the platinum re-dispersion of the reforming catalyst may be improved by controlling the time of the re-dispersion process within the small-scale reactor. For example, the time of the re-dispersion reaction may be adjusted to be in the range of about 0.1 hours to about 5 hours, about 1 hour to about 4 hours, or about 2 hours to about 3 hours. I some embodiments, the time of the re-dispersion reaction may be adjusted to be about 4 hours or less, about 3.5 hours or less, about 3 hours or less, about 2 hours or less, or about 1 hour or less.
As noted herein above, any of the above mentioned oxychlorination conditions may be adjusted, in particular, to provide enhanced platinum dispersion on the re-dispersed reforming catalyst, enhanced activity of the re-dispersed reforming catalyst, and/or enhanced selectivity of the re-dispersed reforming catalyst, and/or an increase in unit yield when using the re-dispersed reforming catalyst in a CCR reformer system for reforming as described herein. Such enhancement is understood to be described in comparison to activity under other tested conditions. In other embodiments, the oxychlorination conditions may be controlled and/or fixed at a desired level in the small-scale reactor so as to evaluate and compare the platinum dispersion on various reforming catalysts when subjected to those particular conditions.
As noted above, some aspects of the disclosure provide methods of operating a CCR reformer system for reforming. In some embodiments, the CCR reformer system may comprise a reaction section, a regeneration section, and a halogen recovery section. In some embodiments, each of these individual sections may comprise one or more zones. For example, in some embodiments, the regeneration section includes a burn zone, a halogenation zone, and a drying zone in serial progression. In other embodiments, the burn zone, the halogenation zone, and the drying zone may be in a stacked arrangement, for example, with the burn zone on top such that the catalyst progresses through each of the individual beds under gravity flow.
FIG. 2 illustrates a CCR reformer system for reforming. The process is generally designed for regeneration of a reforming catalyst that is used in a reaction section, e.g., at operation 10. Following the reaction section, the reforming catalyst is passed to a regeneration section 20. Generally, the regeneration section 20 may include one or more regeneration towers 22. The regeneration towers may vary in size and shape and/or in material construction. Typically, any type of regeneration tower typically used in the art may be suitable. As noted above and as depicted in FIG. 2, the regeneration section 20 may include a burn zone 24, halogenation (oxychlorination) zone 26, and drying zone 28. Generally, the catalyst particles, containing a platinum group metal and having coke deposited thereon, are transferred to the burn zone 24 and the catalyst particles are contacted with an oxygen-containing regeneration gas to combust coke from the particles.
Next, the catalyst particles are passed from the burn zone 24 to halogenation zone 26 and the catalyst particles are contacted with a halogen-containing gas in the halogenation zone, re-dispersing the platinum group metal on said reforming catalyst. The halogen-containing gas may vary, however, it typically comprises at least a chloride component. The halogen-containing gas may be added to any of the zones via line 32 to increase the chloride content on the catalyst. While in the halogenation zone 26, the halogen-containing gas from halogenation gas outlet 38 is continuously circulated to a halogenation gas inlet 32 in the halogenation zone 26 via a halogen recovery system 30 and a halogen is added to the halogenation zone 26 in an excess amount to maintain an excess halogen concentration on the surface of the catalyst in the halogenation zone 26. For example, halogen is added to the halogenation zone in an excess amount via line 34, in addition to line 32, to maintain an excess halogen concentration in the halogenation zone 26. In some embodiments, the halogen concentration on the surface of the catalyst in the halogenation zone may be maintained between about 0.5 weight percent to about 1.5 weight percent, about 0.7 weight percent to about 1.3 weight percent, or about 1.0 weight percent to about 1.2 weight percent. In some embodiments, the halogen concentration on the surface of the catalyst in the halogenation zone may be maintained above 0.7 weight percent, above 1.0 weight percent, above 1.2 weight percent, or above 1.3 weight percent. Preferably, the halogen concentration on the surface of the catalyst may be maintained in the range of about 1.0 weight percent to about 1.5 weight percent.
It should be noted that the introduction of the halogen-containing gas in an excess amount advantageously increases the halogen concentration on the surface of the reforming catalyst and thereby, the platinum re-dispersion on the reforming catalyst, which may lead to higher activity and/or selectivity as well as providing a longer lifetime for the CCR catalyst within the system. Generally, the amount of halogen (e.g., chloride) on the catalyst surface and in the gas phase (e.g., the halogen concentration in the halogen-containing gas) can be controlled to maintain peak activity of the reforming catalyst. In some embodiments, the halogen levels on the surface of the reforming catalyst may be controlled by controlling the concentration of halogen in the halogen-containing gas that is continuously circulated within the halogenation zone of the regenerator. In some embodiments, the moisture content and/or the temperature of the halogen-containing gas circulated may also affect the halogen concentration on the surface of the catalyst.
Finally, the catalyst particles may be passed from the halogenation zone 26 to a drying zone 28 and the catalyst particles may be contacted with a drying gas in the drying zone 28. Generally, the drying gas is a heated gas that contacts the catalyst particles and drives moisture from the reforming catalyst. Typically, air or an oxygen-containing gas enters the drying zone as the drying medium and passes upward through the halogenation zone 26 to the burn zone 24 to provide combustion gas. Following the drying zone 28, the catalyst particles are recycled back to reaction section 10 via line 36 and reused in the process.
Having the benefit of the teachings presented in the foregoing descriptions and the examples to follow, many modifications and other embodiments of the disclosure set forth herein will come to mind to those skilled in the art to which these disclosures pertain. Therefore, it is to be understood that the disclosure is not to be limited to the specific embodiments disclosed and that modifications and other embodiments are intended to be included within the scope of the appended claims. Although specific terms are employed herein, they are used in a generic and descriptive sense only and not for purposes of limitation.

EXPERIMENTAL

Experiments were conducted with commercial reforming catalysts in a small-scale reactor. The oxychlorination conditions within the small-scale reactor were controlled to evaluate platinum dispersion on the re-dispersed reforming catalysts. The first catalyst evaluated for platinum re-dispersion (referred to herein as “Catalyst A”) is an older generation reforming catalyst. Catalyst A is a spherical, platinum/tin containing reforming catalyst promoted on a low density alumina support, which is commercially available from Axens SA®, for example, as the PS-40™ reforming catalyst. Two newer generation reforming catalysts were also evaluated for platinum re-dispersion (referred to herein as “Catalyst B” and “Catalyst C” respectively). Catalyst B is a multi-metallic, platinum/tin containing reforming catalyst promoted on a low density alumina support, which is commercially available from Axens SA®, for example, as the Symphony® PS-100 reforming catalyst. Catalyst C is a spherical, multi-metallic, platinum/tin containing reforming catalyst promoted on a high purity alumina support, which is commercially available from Axens SA®, for example, as the Symphony® PS-110. It should be noted that the particular catalyst samples tested, and the subsequent data and analysis provided herein, is merely presented by way of example and generally any CCR reforming catalyst suitable for use in a CCR reformer system may be evaluated according to the methods and systems described herein.
Initially, each of the catalysts were subjected to a steam deactivation process, resulting in agglomeration of the platinum contained on the catalysts. Each agglomerated catalyst sample was then treated with a chloride source (HCl) and subjected to a re-dispersion process conducted under controlled oxychlorination conditions in a small-scale reactor. Various oxychlorination conditions were controlled and evaluated during the re-dispersion process to determine their effect on the platinum dispersion on the re-dispersed catalysts. The following parameters were found to affect the platinum re-dispersion of the reforming catalysts tested: catalyst chloride level, temperature, oxygen level, and time. Data regarding the effect of these parameters on the platinum re-dispersion of the tested catalysts is provided in the examples herein below. All platinum dispersion values presented therein are in reference to the platinum dispersion percentage, for example, as defined herein above.

Example 1

Re-dispersion experiments were conducted on Catalyst A and Catalyst B in a small-scale reactor at 550° C. with 21% oxygen for 4 hours. Catalyst chloride levels were varied between 0.7 and 1.2 wt. % Cl to determine the effect of catalyst chloride level on platinum dispersion in the tested catalysts. As demonstrated in Table 1 below, platinum dispersion improved when catalyst chloride levels were increased to 1.0 wt. % Cl and further improved significantly when catalyst chloride levels were increased to 1.2 wt. % Cl. Similar improvements were observed for both Catalyst A and Catalyst B. However, Catalyst A displayed higher platinum dispersion after treatment than Catalyst B.

TABLE 1

		A	B

	0.7 wt. % Cl		20%
	1.0 wt. % Cl	59%	32%
	1.2 wt. % Cl	98%	79%

Example 2

Re-dispersion experiments were conducted on Catalysts A, B and C in a small-scale reactor for 4 hours with 21% oxygen with a catalyst chloride level of 1.2 wt. % Cl. Temperature was varied between 468° C. to 550° C. within the reactor to determine the effect of temperature on platinum dispersion in the tested catalysts. As demonstrated in Table 2, all catalyst systems generally displayed improved platinum dispersion values when higher temperatures were used. In fact, Catalyst A experienced 100% platinum dispersion when subjected to a temperature of 550° C.

TABLE 2

		A	B	C

	468° C. (875° F.)	73%	64%	45%
	510° C. (950° F.)	83%	81%	69%
	550° C. (1022° F.)	100%	79%	82%

Example 3

Re-dispersion experiments were conducted on Catalyst A in a small-scale reactor at 550° C. for 4 hours with a catalyst chloride level of 1.2 wt. % Cl. The oxygen level was varied to between 7% and 21% within the reactor to determine the effect of oxygen level on platinum dispersion in the tested catalysts. As demonstrated in Table 3, platinum dispersion remained low until the oxygen content was increased to 21% oxygen; for example, the platinum dispersion increased from 25% to 98% when the oxygen level was increased from 18% to 21% oxygen.

TABLE 3

		A

	7% oxygen	22%
	18% oxygen	25%
	21% oxygen	98%

Example 4

Re-dispersion experiments were conducted on Catalysts A, B, and C in a small scale reactor at 550° C. with an oxygen content of 21% and a catalyst chloride level of 1.2 wt. % Cl. To evaluate how time affects platinum re-dispersion, the re-dispersion procedure was conducted using regeneration times between 1 and 4 hours. In a commercial CCR unit, it takes approximately 4 hours for the reforming catalyst to pass through the regenerator. Therefore, it is desirable to complete the dispersion in less than 4 hours. As demonstrated in Table 4, all three catalysts tested displayed reasonable platinum dispersion values after a re-dispersion time of 1 hour (e.g., all having platinum dispersion of at least 67%). In addition, platinum dispersion values displayed a further increase as the time was extended to 2 hours and 4 hours in both Catalyst A and C. Catalyst B showed a decrease in platinum dispersion from 1 hour to 2 hours (likely due to error). Generally, as demonstrated in Table 4, Catalyst A achieved 98% platinum dispersion, while Catalyst B and Catalyst C showed slightly lower platinum dispersion values (79% for Catalyst B and 82% for Catalyst C) after four hours.

TABLE 4

		A	B	C

	1 hr	79%	72%	67%
	2 hr	86%	56%	67%
	4 hr	98%	79%	82%

This is a divisional of U.S. Non-Provisional application Ser. No. 16/869,186, filed May 7, 2020, titled “METHODS AND REFORMING SYSTEMS FOR RE-DISPERSING PLATINUM ON REFORMING CATALYST,” which claims priority to and the benefit of U.S. Provisional Application No. 62/845,485, filed May 9, 2019, titled “RE-DISPERSING PLATINUM ON REFORMING CATALYST,” the disclosures of which are incorporated herein by reference in their entirety.
Although only a few exemplary embodiments have been described in detail herein, those skilled in the art will readily appreciate that many modifications are possible in the exemplary embodiments without materially departing from the novel teachings and advantages of the embodiments of the present disclosure. Accordingly, all such modifications are intended to be included within the scope of the embodiments of the present disclosure as defined in the following claims.

Claims

1. A method of operating a continuous catalyst regeneration reformer system, the system having a regeneration section, the regeneration section includes a burn zone, a halogenation zone, and a drying zone, the method comprising:

(a) transferring catalyst particles comprising a platinum group metal and having coke deposited thereon to the burn zone to contact the catalyst particles with an oxygen-containing regeneration gas thereby to combust the coke from the catalyst particles;

(b) passing the catalyst particles from the burn zone to the halogenation zone to contact the catalyst particles with a halogen-containing gas in the halogenation zone;

(c) re-dispersing the platinum group metal on the catalyst particles;

(d) continuously circulating the halogen-containing gas from a halogenation gas outlet to a halogenation gas inlet in the halogenation zone to maintain a halogen concentration on the surface of the catalyst particles of at least about 1.0 weight percent; and

(e) passing the catalyst particles from the halogenation zone to a drying zone to contact the catalyst particles with a drying gas in the drying zone.

2. The method of claim 1, wherein the burn zone, the halogenation zone, and the drying zone are in a serial arrangement.

3. The method of claim 1, wherein the burn zone, the halogenation zone, and the drying zone are in a stacked arrangement.

4. The method of claim 3, wherein the catalyst particles pass from the burn zone to the halogenation zone under gravity flow.

5. The method of claim 3, wherein the catalyst particles pass from the halogenation zone to the drying zone under gravity flow.

6. The method of claim 1, wherein the halogen concentration on the surface of the catalyst particles is maintained at a concentration above about 1.2 weight percent.

7. The method of claim 1, wherein the halogen concentration on the surface of the catalyst particles is maintained in a range of about 1.0 weight percent to about 1.5 weight percent.

8. The method of claim 1, wherein the halogenation zone further comprises a halogenation recovery system.

9. The method of claim 1, wherein the regeneration section comprises one or more regeneration towers.

10. The method of claim 1, wherein the continuous catalyst regeneration reformer system further comprises a reaction section.

11. The method of claim 10, wherein the catalyst particles are recycled into the reaction section following step (e).

12. The method of claim 10, wherein the platinum group metal is selected from the group consisting of platinum, iridium, rhodium and palladium, and wherein the drying gas comprises an oxygen-containing gas.

13. The method of claim 8, wherein the halogen-containing gas comprises a halogen selected from the group consisting of fluorine, chlorine, bromine and iodine.

14. A method of operating a continuous catalyst regeneration reformer system, the system having a regeneration section, the regeneration section includes a burn zone, a halogenation zone, and a drying zone, the method comprising:

(a) transferring catalyst particles comprising a platinum group metal and having coke deposited thereon to the burn zone to contact the catalyst particles with an oxygen-containing regeneration gas thereby to combust the coke from the catalyst particles, the platinum group metal being selected from the group consisting of platinum, iridium, rhodium and palladium;

(c) re-dispersing the platinum group metal on the catalyst particles;

15. The method of claim 14, wherein the burn zone, the halogenation zone, and the drying zone are in a serial arrangement.

16. The method of claim 14, wherein the burn zone, the halogenation zone, and the drying zone are in a stacked arrangement.

17. The method of claim 16, wherein the catalyst particles pass from the burn zone to the halogenation zone under gravity flow, and wherein the catalyst particles pass from the halogenation zone to the drying zone under gravity flow.

18. The method of claim 14, wherein the halogen concentration on the surface of the catalyst particles is maintained at a concentration above about 1.2 weight percent.

19. The method of claim 14, wherein the halogen concentration on the surface of the catalyst particles is maintained in a range of about 1.0 weight percent to about 1.5 weight percent.

20. The method of claim 14, wherein the halogenation zone further comprises a halogenation recovery system, wherein the regeneration section comprises one or more regeneration towers, wherein the continuous catalyst regeneration reformer system further comprises a reaction section, and wherein the catalyst particles are recycled into the reaction section following step (e).