EWT Skeletal Molecular Sieve, Its Manufacturing Process and Use

Abstract

The present disclosure relates to various modified EWT framework zeolites, their processes, and uses.

Description

Technical Field

[0001] Cross - reference to related applications This application claims priority and the benefit thereof to European Application No. 22183386.6 filed on July 6, 2022, the entire disclosure of which is incorporated herein by reference.

[0002] Field The present disclosure relates to EWT framework molecular sieves, a manufacturing process of the molecular sieves, and the use of these molecular sieves. More particularly, the present invention relates to a process for increasing the concentration of aluminum in an EWT framework molecular sieve.

Background Art

[0003] Background EWT framework molecular sieves include zeolites such as EMM - 23. EMM - 23 is a crystalline or substantially crystalline material. EMM - 23 is described as a molecular sieve in U.S. Patent No. 9,205,416, the entire content of which is incorporated herein by reference. The framework structure has been approved by the Structure Commission of the International Zeolite Association and is described in the zeolite structure database. Molecular sieves can be used as adsorbents, catalysts, or carriers for catalysts, especially for hydrocarbon conversion. EMM - 23 has a crystal structure that can be identified by X - ray diffraction (XRD) as described in US9,205,416. EMM - 23 has uniform cavities and pores interconnected by channels. The size and dimensions of the cavities and pores enable the adsorption of molecules of a specific size. Due to its ability to adsorb molecules by size selection, EMM - 23 has many applications including hydrocarbon conversion, such as cracking, hydrocracking, disproportionation, alkylation, oligomerization, and isomerization.

[0004] EWT framework molecular sieves such as EMM-23 can be prepared from a mixture of a source of water, hydroxide ions, SiO2, optionally Al, and a structure-directing agent. The structure-directing agent can be an organic molecule, such as a diquaternary ammonium molecule. The as-made molecular sieve prepared from these sources may contain the structure-directing agent within the crystal framework. Heat treatment (e.g., calcination) of the as-made molecular sieve will result in a molecular sieve without the structure-directing agent. Including a trivalent element such as aluminum in the molecular sieve can result in property modifications, such as an increase in acidity, which can improve catalytic activity. It may be difficult to directly synthesize an EWT framework molecular sieve with a desired level of aluminum content. In particular, it has been found that it is difficult to crystallize EMM-23 with a framework SiO2:Al2O3 ratio of less than 100. EMM-23 has been previously described in U.S. Patent No. 9,205,416, and the modification process of EMM-23 is described in US2019 / 0030518A1 and US2019 / 0031519A1, but there is a need for modified materials of EMM-23 with improved properties.

Summary of the Invention

[0005] Abstract The present disclosure provides an improved process for preparing an EWT framework zeolite with an increased aluminum content. More particularly, the present invention relates to a process for increasing the aluminum content of an EWT zeolite by repeated treatment with an aqueous aluminum salt solution. In a first aspect, the present invention is a process for increasing the aluminum content of an EWT framework zeolite and mixtures thereof, the process comprising the following steps: a) contacting the EWT framework zeolite with an aqueous aluminum salt solution; and b) separating the EWT framework zeolite from the aqueous aluminum salt solution and subjecting the EWT framework zeolite to a treatment comprising these steps, And repeating this process such that the EWT framework zeolite undergoes a total of n process cycles, where n is a number in the range of 2 to 10, for the process.

[0006] The inventors have found that the process of the first aspect of the present invention is unexpectedly effective in incorporating aluminum into the EWT framework zeolite, thereby providing an EWT framework zeolite having a specific Si:Al2 ratio of 70 or less. In a second aspect, the present invention provides an EWT framework zeolite having a specific Si:Al2 ratio of 70 or less, produced by the process of the first aspect. In a third aspect, the present invention provides a process for the conversion of an organic compound, the process comprising contacting the organic compound with the EWT framework zeolite of the second aspect. EMM-23 is a preferred EWT framework zeolite. As used herein, the specific SiO2:Al2O3 and Si:Al2 ratios have the same meaning and are molar ratios. Any two or more features described in this specification, including this summary section, can be combined to form combinations of features not specifically described herein. Details of one or more features are specified in the accompanying drawings and the following description. Other features and advantages will be apparent from the following description and drawings, as well as from the claims.

Brief Description of the Drawings

[0007]

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Mode for Carrying Out the Invention

[0008] Detailed Description In this specification, various modified EWT framework zeolites, the preparation processes of these zeolites, and their uses are provided. The as-prepared EWT framework zeolite (i.e., before heat treatment or other treatment for removing the structure-directing agent (SDA), sometimes referred to herein as "as-synthesized" or "as-prepared") may contain a structure-directing agent (SDA) as one of the synthetic reagents. The heat treatment (e.g., calcination) of the as-prepared EMM-23 typically exposes the material to a high temperature, e.g., 400 - 600 °C, in an atmosphere selected from air, nitrogen, or a mixture thereof to remove the SDA. The heat-treated (e.g., calcined) form of the EWT framework zeolite may be described as having a chemical composition of an oxide of a trivalent element (e.g., Al2O3) and an oxide of a tetravalent element (e.g., SiO2), and these oxides can be in various molar ratios.

[0009] The concentration of aluminum in zeolite is often expressed in terms of the molar ratio of silica to alumina, i.e., the SiO2:Al2O3 ratio. It is often abbreviated as the Si:Al2 ratio, and for the purposes of this disclosure, the expressions Si:Al2 and SiO2:Al2O3 should be interpreted as equivalent. The concentration of aluminum in zeolite may also be expressed as the ratio of silicon atoms to aluminum atoms, i.e., Si:Al. The ratio expressed as Si:Al is numerically half of the ratio expressed as Si:Al2. For example, a ratio of Si:Al = 75 corresponds to Si:Al2 of 150.

[0010] Incorporation of additional aluminum This specification provides additional modified EWT framework zeolites that contain a relatively large amount of aluminum. Modified EWT framework zeolites with more aluminum are more stable than materials with less aluminum during heat treatment (e.g., calcination) or in their final heat-treated form. It may be difficult to prepare EWT framework zeolites having an atomic ratio of Si to Al of less than 75 (e.g., Si:Al of less than 75 corresponding to Si:Al2 of less than 150), such as EMM-23 zeolite. One possible route to incorporate more aluminum into the EWT framework zeolite is to increase the amount of aluminum source(s) in the mixture to prepare the as-made EWT framework zeolite. However, in practice, the process does not incorporate much additional aluminum into the EWT framework zeolite, and the reproducibility of this synthesis appears to be sensitive to the presence of aluminum and can result in undesirable impurities. This specification describes aluminum-modified EWT framework zeolites having a molar ratio of Si:Al2 of less than 70, prepared by a process that includes the step of incorporating Al into an EWT framework zeolite (i.e., an already prepared EWT framework zeolite) by repeated cycles of treatment with an aqueous aluminum salt solution.

[0011] In the process of the first aspect of the present invention, steps a) and b) are performed in that order. Performing steps a) and b) once constitutes a processing cycle. When the steps are performed only once, there is only one process and n = 1. The inventors have found that the amount of additional aluminum incorporated into the zeolite tends to decrease as the number of cycles increases. In the method of the present invention, the processing cycle is repeated at least once and at most nine times after the first time, and as a result, the total number of processing cycles n is in the range of 2 to 10. Optionally, n is in the range of 2 to 8, and optionally in the range of 3 to 6. In step a), the contact time during which the EWT framework zeolite is contacted with the aqueous aluminum salt solution may be any suitable duration. Optionally, in step a), the EWT framework zeolite is contacted with the aqueous aluminum salt solution for a duration in the range of 0.25 hours to 24 hours, optionally 1 hour to 24 hours, and optionally 2 hours to 6 hours. Any aluminum salt that is at least partially soluble in water can be used for the treatment. Preferably, the aluminum salt is soluble in water at 25 ° C to at least 0.05 wt%, preferably at least 0.1 wt%. Suitable salts can be selected from Al(NO3)3, Al2(SO4)3, AlCl3, (NH4)3AlF6, or mixtures thereof. For example, the aluminum salt can contain or be Al(NO3)3.

[0012] Each processing cycle of the process of the first aspect of the present invention may independently optionally include one or more additional steps. Optionally, in one or more processing cycles, the process also includes, after step b), c) a step of washing the EWT framework zeolite with a washing liquid. Optionally, in all processing cycles, the process also includes, after step b), c) a step of washing the EWT framework zeolite with a washing liquid. Typically, the cleaning liquid will be an aqueous solution. For example, the cleaning liquid can be water, particularly water having a pH between 6.0 and 8.0. The cleaning liquid can be appropriately selected from distilled water and deionized water. Alternatively, the cleaning liquid can be an alkaline aqueous solution, such as an aqueous ammonium hydroxide solution or, for example, a hydroxide of an alkali metal or an alkaline earth metal (followed by an exchange with ammonium ions including, for example, NH4 + + , tetraalkylammonium, such as tetramethylammonium, tetraethylammonium, tetrapropylammonium, and so-called dicquats, such as C3, C4, C5, or C6 dicquats), and can preferably be an aqueous ammonium hydroxide solution. The use of an alkaline cleaning liquid such as an aqueous ammonium hydroxide solution promotes the removal of octahedrally coordinated aluminum, and this removal can lead to greater selectivity in any reaction in which the zeolite is used as a catalyst. However, contact with an alkaline solution also tends to reduce the crystallinity of the zeolite, so the pH of the alkaline cleaning liquid and the duration and conditions of the cleaning step must be selected to avoid excessive decomposition of the crystal structure. If more than one treatment cycle includes cleaning step c), different cleaning liquids can be used in different cycles. For example, some treatment cycles can use neutral water having a pH between 6.0 and 8.0, and other treatment cycles can use an alkaline cleaning liquid, such as an aqueous ammonium hydroxide solution. Optionally, at least one treatment cycle includes cleaning step c) where the cleaning liquid is alkaline, such as an aqueous ammonium hydroxide solution.

[0013] Separation step b) may involve separating the EWT framework zeolite from the aqueous aluminum salt solution by any suitable technique. For example, the separation may involve filtration or centrifugation. Separation step b) will typically remove at least 90 wt% of the aqueous aluminum salt solution, preferably substantially all of the aqueous aluminum salt solution, leaving the zeolite as a wet solid. As described above, the wet solid may then undergo an optional washing step c). Optionally, the wet solid may undergo an optional step d) of drying the EWT framework zeolite. Drying step d) may be carried out immediately after step b) if there is no washing step c), or may be carried out after washing step c) if washing step c) is present.

[0014] Optional drying step d) may involve contact with hot air at a temperature in the range of, for example, 40°C to 200°C, optionally 50°C to 100°C. The duration of the drying step may optionally be from 1 hour to 24 hours, for example, 3 hours to 12 hours. Typically, the final treatment cycle will include a drying step d) to leave the zeolite as a dry zeolite at the end of the process. Optionally, only the final treatment cycle includes drying step d). Contact step a) may be carried out in any suitable vessel. For example, step a) may be carried out as a batch process in a stirred tank reactor. Advantageously, step a) is carried out at a temperature above 40°C, preferably in the range of 50°C to 100°C, more preferably in the range of 60°C to 95°C. Step a) can be carried out at high pressure, for example, in an autoclave, but it will generally be convenient to carry out step a) at ambient atmospheric pressure in order to raise the temperature above 100°C.

[0015] Optionally, the EWT framework zeolite is an uncalcined or "as-made" EWT framework zeolite. Such an uncalcined or as-made zeolite will typically contain an amount of structure-directing agent (SDA) within its pore structure. When the EWT framework zeolite is an uncalcined or "as-made" EWT framework zeolite, the process of the present invention may include a step of calcining the zeolite to remove the SDA after the final treatment cycle. Alternatively, the EWT framework zeolite used in the process of the first aspect of the present invention is a calcined EWT framework zeolite. Preferably, the EWT framework zeolite is EMM-23, optionally a calcined EMM-23. The EWT framework zeolite used in the process of the first aspect of the present invention can be in any suitable form. For example, the EWT framework zeolite can be in the form of unbound zeolite crystals. Alternatively, the EWT framework zeolite can be in the form of pellets or granules containing a binder.

[0016] As described above, in a second aspect, the present invention provides an EWT framework zeolite produced by the process of the first aspect, wherein the ratio of Si:Al2 is 70 or less. Optionally, the ratio of Si:Al2 is 60 or less, optionally 55 or less. Optionally, the ratio of Si:Al2 is at least 15, optionally at least 20. The ratio of Si:Al2 can be from 15 to 70, for example from 20 to 60. As described above, in a third aspect, the present invention provides a process for converting an organic compound into a conversion product, the process comprising contacting the organic compound with the EWT framework zeolite of the second aspect. Preferably, the EWT framework zeolite of the second aspect of the present invention is EMM-23.

[0017] The EMM-23 used in the process of the first aspect of the present invention may be substantially free of one or more impurities, such as zeolite beta, ZSM-5, or a mixture thereof (e.g., at least 50% by mass, at least 60% by mass, at least 70% by mass, at least 80% by mass, at least 90% by mass, at least 95% by mass, at least 97% by mass, or at least 99% by mass of EMM-23 (i.e., a mass percentage based on the total mass of the material that is EMM-23 and not an impurity) is free of impurities). The EMM-23 used in this process may be substantially free of one or more impurities, and as a result, other phases such as zeolite beta, ZSM-5, or a mixture thereof cannot be identified in the XRD pattern of the modified EMM-23 material.

[0018] EMM-23 can have an alpha value greater than 10. The alpha value of EMM-23 can be greater than 20, greater than 30, greater than 40, or greater than 50. In some embodiments, the alpha value can be 15 - 50, 20 - 40, or 30 - 35. EMM-23 can have a micropore volume greater than 0.15 cc / g. The micropore volume can be 0.15 - 0.30, 0.25 - 0.30 cc / g, or 0.20 - 0.30 cc / g. EMM-23 can have a lattice cell a parameter of 19.6 ± 0.5 Å and a c parameter of 13.5 ± 0.5 Å. EMM-23 has at least 4 XRD peaks having 2θ degree values optionally selected from Table 1 below.

[0019] Table 1

Table 1

[0020] EMM-23 has at least 4 XRD peaks having 2θ degrees and interplanar spacing d values optionally selected from Table 2 below, where the interplanar spacing d value has a deviation determined based on a 2θ degree corresponding to a deviation of ±0.20 when converted to a corresponding value using Bragg's law for the interplanar spacing d.

[0021] Table 2

Table 2

[0022] Optionally, EMM-23 has at least 5 or 6 XRD peaks selected from Table 1 or Table 2. EMM-23 can have at least 4, at least 5, or 6 XRD peaks having 2θ values selected from Table 1 or 2 and a micropore volume greater than 0.15 cc / g (e.g., 0.15 - 0.30, 0.25 - 0.30 cc / g, or 0.20 - 0.30 cc / g), or a unit cell a parameter of 19.6 ± 0.5 Å and a c parameter of 13.5 ± 0.5 Å. Optionally, EMM-23 has at least 4 XRD peaks having 2θ degree values selected from Table 3.

[0023] Table 3

Table 3

[0024] Optionally, EMM-23 has at least 4 XRD peaks having 2θ degree values and interplanar spacing d values selected from Table 4. Here, the interplanar spacing d value has a deviation determined based on a 2θ degree with a corresponding deviation of ±0.20 when converted to the corresponding value using Bragg's law for the interplanar spacing d.

[0025] Table 4

Table 4

[0026] Optionally, EMM-23 has at least 5, at least 6, at least 7, at least 8, at least 9, or 10 XRD peaks having 2θ degree values selected from Table 3 or Table 4. EMM-23 has at least 4, at least 5, at least 6, at least 7, at least 8, at least 9, or 10 XRD peaks having 2θ degree values selected from Table 3 or Table 4 and a micropore volume greater than 0.15 cc / g (e.g., 0.15 - 0.30, 0.25 - 0.30 cc / g, or 0.20 - 0.30 cc / g), or a unit cell a parameter of 19.6 ± 0.5 Å and a c parameter of 13.5 ± 0.5 Å. Optionally, EMM-23 has at least 4 XRD peaks having 2θ degree values selected from Table 5.

[0027] Table 5

Table 5

[0028] Optionally, EMM-23 has at least 4 XRD peaks having 2θ degree values and interplanar spacing d values selected from Table 6. Here, the interplanar spacing d value has a deviation determined based on 2θ degrees with a corresponding deviation of ±0.20 when converted to the corresponding value using Bragg's law for the interplanar spacing d.

[0029] Table 6

Table 6

[0030] EMM-23 has at least 5, at least 6, at least 7, at least 8, at least 9, at least 10, at least 11, or 12 XRD peaks having 2θ degree values optionally selected from Table 5 or Table 6. EMM-23 has at least 4, at least 5, at least 6, at least 7, at least 8, at least 9, at least 10, at least 11, or 12 XRD peaks having 2θ degree values optionally selected from Table 5 or Table 6 and a micropore volume of more than 0.15 cc / g (for example, 0.15 - 0.30, 0.25 - 0.30 cc / g, or 0.20 - 0.30 cc / g), or a unit cell a parameter of 19.6 ± 0.5 Å and a c parameter of 13.5 ± 0.5 Å. To avoid misunderstanding, the XRD peaks of EMM-23 of the present invention may have intensities different from those described in Tables 1 - 6 above.

[0031] As described above, in the second aspect, the present invention provides an EWT framework zeolite produced by the process of the first aspect, wherein the EWT framework zeolite has a Si:Al2 ratio of 70 or less. Optionally, the Si:Al2 ratio is 60 or less, and optionally 55 or less. Optionally, the Si:Al2 ratio is at least 15, and optionally at least 20. The Si:Al2 ratio can be 15 - 70, for example 20 - 60. In a preferred embodiment, the EWT framework zeolite of the second aspect of the present invention is EMM-23. The EMM-23 of the second aspect of the present invention will have a modified XRD pattern, but may also retain some identical XRD peaks having the same 2θ degree values and / or interplanar spacing d values as described above for the EMM-23 used in the process of the first aspect with reference to Tables 1 - 6 optionally.

[0032] Preparation of EMM-23 As-prepared EMM-23 (for example, the material before heat treatment to remove the SDA) can be prepared from a mixture of water, hydroxide ions, Si, optionally Al, and optionally a source of the structure-directing agent SDA. For example, the molar ratios in the mixture can be as follows: SiO2 / Al2O3 can be at least 5 (e.g., at least 100, at least 1000, or all SiO2); H2O / SiO2 can be from 0.5 to 50 (e.g., from 2 to 10 or from 14 to 40); OH - / SiO2 can be from 0.1 to 1.0 (e.g., from 0.2 to 0.5); and SDA / SiO2 can be from 0.05 to 0.5 (e.g., from 0.1 to 0.25).

[0033] In one or more embodiments, the molar ratios of these sources in as-made EMM-23 that are subsequently heat treated to give calcined EMM-23 can be as follows: SiO2 / Al2O3 can be equal to or at least 75 (e.g., at least 100, at least 1000, or all SiO2); H2O / SiO2 can be from 0.5 to 50 (e.g., from 2 to 10 or from 14 to 40); OH - / SiO2 can be from 0.1 to 1.0 (e.g., from 0.2 to 0.5); and SDA / SiO2 can be from 0.05 to 0.5 (e.g., from 0.1 to 0.25).

[0034] In one or more embodiments, the as-made EMM-23 material can be prepared by mixing an Al source with an SDA hydroxide solution and then subsequently adding a Si source to the mixture to form a base mixture of these components. A seed of the EMM-23 material can be added to the base mixture. The solvent of the base mixture (e.g., water from the hydroxide solution and optionally methanol and ethanol from the hydrolysis of the silica source) can be removed (e.g., by evaporation or lyophilization) such that the desired molar ratio of solvent to SiO2 is achieved for the resulting mixture. When too much water is removed during the solvent removal process, water can be added to the resulting mixture to achieve the desired H2O / SiO2 molar ratio. The mixture is then sealed within a suitable reaction vessel, e.g., within a steel Paar autoclave. The sealed mixture is heated such that the sealed mixture is maintained (e.g., within a sealed autoclave placed within a convection oven maintained at 150 °C for 1 day to 14 days) for a sufficient time at a temperature sufficient for the formation of EMM-23 crystals, optionally with rotation or stirring. The detailed procedure for the preparation of the as-made EMM-23 material can also be found in U.S. Patent No. 9,205,416, the entire content of which is hereby incorporated by reference.

[0035] Examples of Si sources can be selected from silica, precipitated silica, fumed silica, alkali metal silicates, and / or colloidal suspensions of tetraalkyl orthosilicates (e.g., tetraethyl orthosilicate, tetramethyl orthosilicate, etc.). Examples of various sources of silica include Ludox® (e.g., LUDOX® AS-40) colloidal silica, precipitated silica, e.g., products from Ultrasil®, SIPERNAT®, and HI-SIL®, Carbosperse™ fumed silica suspensions, and CAB-O-SIL® fumed silica, or mixtures thereof.

[0036] The Al source can contain aluminum or be Al, and other suitable sources of aluminum can be selected from aluminum hydride, aluminum hydroxide, alkali metal aluminates, aluminum alkoxides, and water-soluble aluminum salts such as aluminum nitrate. Suitable sources of structure-directing agents can be selected from relevant diquaternary ammonium compounds, such as hydroxides and / or salts of 1,5-bis(N-propylpyrrolidinium)pentanedication, 1,6-bis(N-propylpyrrolidinium)hexanedication, 1,4-bis(N-methylpyrrolidinum)butanedication.

[0037] In one or more embodiments, after solvent adjustment (e.g., achieving the desired molar ratio of water to silica), the mixture can be mixed by mechanical processes such as stirring or high-shear blending to ensure proper homogenization of the base mixture. For example, a FlackTek seed mixer can be used at a mixing speed of 1800 - 2200 rpm (e.g., 2000 rpm) to improve the homogenization of the base mixture. Depending on the nature of the reagents in the base mixture, the amount of solvent (e.g., water) in the mixture before crystallization can be reduced to obtain the desired solvent molar ratio (e.g., H2O / SiO2). Suitable methods for reducing the solvent (e.g., water) content include evaporation under static or flowing atmospheres such as ambient air, dry nitrogen, dry air, or spray drying or freeze drying. In one or more embodiments, without removing the solvent from the base mixture, a silica source such as Ludox® (e.g., LUDOX® AS-40), Ultrasil®, Carbosperse™, or a mixture thereof can be used at a mixing speed of 1800 - 2200 rpm (e.g., 2000 rpm) to produce a base mixture having the desired solvent molar ratio (e.g., H2O / SiO2 molar ratio). A high mixing speed such as 2000 rpm can result in homogenization of the mixture even when the mixture has a solvent molar ratio greater than 10 (e.g., 15 - 40) (e.g., H2O / SiO2 molar ratio).

[0038] The crystallization of as-made EMM-23 in the formation of as-made EMM-23 can be carried out in a suitable reaction vessel, such as a polypropylene jar or a Teflon®-lined or stainless-steel autoclave placed in a convection oven maintained at a temperature of about 100 to about 200 °C, under static or stirred conditions, for a time sufficient for crystallization to occur at the use temperature, e.g., for about 1 day to about 14 days. Thereafter, the solid crystals of as-made EMM-23 are separated from the liquid (e.g., by filtration or centrifugation) and recovered. When using SDA during the synthesis of as-made EMM-23, some or all of it can be removed to form calcined EMM-23. The removal of SDA can be carried out using a heat treatment (e.g., calcination) in which the as-made EMM-23 material is heated at a temperature sufficient to remove some or all of the SDA in an atmosphere selected from air, nitrogen, or a mixture thereof. Sub-atmospheric pressure may be utilized for the heat treatment, but atmospheric pressure is desirable for reasons of convenience. The heat treatment can be carried out at a temperature up to 650 °C, e.g., 400 - 600 °C. The heat treatment (e.g., calcination) can be carried out in a box furnace in dry air exposed to a drying tube containing a desiccant to remove water from the air. The heat-treated EMM-23 material (e.g., the calcined product) can serve as a catalyst for the conversion reaction of certain organic compounds, e.g., hydrocarbons.

[0039] EWT framework zeolite (e.g., as-made, calcined, modified, unmodified, or any other form of EWT framework zeolite) can be mixed with a hydrogenation component. The hydrogenation component can be selected from molybdenum, tungsten, rhenium, nickel, cobalt, chromium, manganese, or noble metals such as platinum or palladium, etc., and the hydrogenation-dehydrogenation function will be achieved. The hydrogenation component can be incorporated into the composition through one or more of the following processes: co-crystallization; incorporating Group IIIA elements, such as aluminum, to a certain extent in the structure; impregnating into the composition; or physically mixing with the composition. For example, the hydrogenation component can be impregnated into the EWT framework zeolite. In the case of platinum, the EWT framework zeolite can be impregnated with a solution containing platinum metal-containing ions. Platinum compounds suitable for impregnation can be selected from chloroplatinic acid, platinous chloride, and platinum amine complex-containing compounds. Combinations of all the above-described aspects, such as the use of heat and vacuum, are efficient processes for at least partially dehydrating the EWT framework zeolite.

[0040] EWT framework zeolite (e.g., as-made, calcined, modified, unmodified, or any other form of EWT framework zeolite) can be at least partially dehydrated when used as an adsorbent or as a catalyst. The dehydration can be achieved by heating the EMM-23 at a temperature in the range of 200 - 370 °C in an ambient atmosphere (the atmosphere can be selected from air, nitrogen, or their mixture) at a pressure of atmospheric pressure, less than atmospheric pressure, or greater than atmospheric pressure for 30 minutes to 48 hours. Dehydration can also be carried out at room temperature by placing the EWT framework zeolite in a vacuum, but a longer time is required to achieve a sufficient amount of dehydration. Combinations of all the above-described aspects, such as the use of heat and vacuum, are efficient processes for at least partially dehydrating the EWT framework zeolite.

[0041] As described above, in the third aspect, the present invention provides a process for converting an organic compound into a conversion product, the process comprising the step of contacting the organic compound with the EWT framework zeolite of the second aspect. EWT framework zeolites, such as EMM-23 (e.g., as-made, calcined, modified, unmodified, or in any other form of EWT framework zeolite), can be used as adsorbents or in aluminosilicate form as catalysts to catalyze a variety of organic compound conversion processes. Examples of chemical conversion processes effectively catalyzed by the treated EWT framework zeolite of the second aspect of the present invention, either alone or in combination with one or more other catalytically active substances (including other crystalline catalysts), include those that require a catalyst with acid activity. Examples of organic conversion processes that can be catalyzed by the EWT framework zeolite of the second aspect of the present invention include decomposition, hydrocracking, disproportionation, alkylation, oligomerization, and isomerization.

[0042] EWT framework zeolites (e.g., as-made, calcined, modified, unmodified, or in any other form of EWT framework zeolite) can be incorporated with another material resistant to the temperatures and other conditions utilized in organic conversion processes. The resistant material can be selected from active materials, inert materials, synthetic zeolites, zeolites of natural origin, inorganic materials, or mixtures thereof. Examples of the resistant material can be selected from clays, silica, metal oxides, such as alumina, or mixtures thereof. The inorganic material can be of natural origin or in the form of a gelatinous precipitate or gel, such as a mixture of silica and metal oxides. Using a resistant material in combination with EWT framework zeolites, i.e., in combination with as-made zeolite crystals (which are active) or present during their synthesis, tends to change the conversion rate and / or selectivity of the catalyst in certain organic conversion processes. Inert resistant materials can function appropriately as diluents to control the amount of conversion in a given process and, as a result, obtain products in an economical and orderly manner without using other means to control the reaction rate. These materials can be incorporated into clays of natural origin, such as bentonite and kaolin, to improve the crushing strength of the catalyst under commercial operating conditions. The inert resistant materials, i.e., clays, oxides, etc., function as catalyst binders. In commercial use, it is desirable to prevent the catalyst from decomposing into a powder-like material, so a catalyst with good crushing strength can be beneficial.

[0043] Natural origin clays that can be complexed with EWT framework zeolites such as EMM-23 include montmorillonite and kaolin family, and these families include subbentonite, and kaolin, and are generally known as Dixie, McNamee, Georgia and Florida clays, and their main mineral components are halloysite, kaolinite, dickite, nacrite or anauxite. The clay can be used in the as-mined untreated state or first calcined, acid-treated or chemically modified. Binders useful for complexing with EWT framework zeolites such as EMM-23 also include inorganic oxides selected from silica, zirconia, titania, magnesia, beryllia, alumina, or mixtures thereof.

[0044] EWT framework zeolites (e.g., as-made, calcined, modified, unmodified, or any other form of EWT framework zeolite) can be complexed with porous matrix materials such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania and ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia. The relative ratios of EWT framework zeolite to inorganic oxide matrix can vary widely, and the EWT framework zeolite content ranges from about 1 to about 90 weight percent of the composite, or when the composite is prepared in the form of beads, ranges from about 2 to about 80 weight percent of the composite.

[0045] In one or more embodiments, embodiments described herein that use the expression "material comprising" with respect to a particular composition are meant to encompass "material comprising or being" the particular composition. As used herein, unless otherwise specified, a numerical value or range of numerical values may deviate to the extent considered reasonable by a person skilled in the relevant art. It is well known that differences in equipment and other characteristics can affect numerical values. Such deviation may be plus or minus 2%, 5%, 10%, 15%, 20%, 25%, or 30% of the indicated numerical value or range of numerical values, unless otherwise specified. As used herein, the term "substantially absent" means that the materials described herein (e.g., EWT framework zeolite) are at least 50%, at least 60%, at least 70%, at least 80%, at least 90%, at least 95%, at least 97%, or at least 99% (e.g., 99.5% or 99.9%) pure EWT framework zeolite material by mass, based on the total mass of the composition, as determined by quantification using XRD or NMR spectroscopy (e.g., by measuring the area or relative intensity of the relevant peak) or by other known methods suitable for such determination. The remainder of the material is non-EWT framework zeolite material, which may be a structure-directing agent, an amorphous material, other impurities, or a mixture thereof.

[0046] As used herein, the term "crystalline" refers to a material in a crystalline solid form and includes, but is not limited to, single-component or multi-component crystalline forms, such as solvates, hydrates, and co-crystals. Crystalline may mean having regularly repeating and / or regularly arranged molecules and having a distinguishable crystal lattice. For example, crystalline EMM-23 may have different water or solvent contents. Different crystal lattices can be identified by methods for characterizing the solid state, such as by XRD (e.g., powder XRD). Other characterization methods known to those skilled in the relevant art are not only further useful for identifying the crystal form but also for determining stability and solvent / water content. As used herein, the term "substantially crystalline" means that the majority (greater than 50%) of the mass of a sample of the described solid material is crystalline and the remainder of the sample is amorphous. In one or more embodiments, a substantially crystalline sample has a crystallinity of at least 95% (e.g., 5% amorphous), at least 96% (e.g., 4% amorphous), at least 97% (e.g., 3% amorphous), at least 98% (e.g., about 2% amorphous), at least 99% (e.g., 1% amorphous), and 100% (e.g., 0% amorphous).

[0047] Analysis methods The elemental composition of the sample was evaluated using inductively coupled plasma (ICP) analysis (ICP-MS) technology combined with mass spectrometry. The sample (50 mg) was first digested at 90 °C in a sealed PTEF vessel with a mixture of aqua regia (a mixture of HCl and HNO3) and HF. Next, H3BO4 was added to neutralize the mixture. The resulting solution was diluted to a 3 jauged volume of 1000 cm and atomized / ionized using a high energy Ar plasma and then accelerated in a mass spectrometer to obtain the mass spectrum of the analytical solution. Solid state NMR measurements were recorded using a Bruker Avance 500 spectrometer with a 4 - mm zirconia rotor and a spinning rate of 14 kHz. A 130.3 MHz short quantitative single pulse (π / 12), a 1 - second recycle delay, and 1856 scans were utilized to obtain the 27 Al MAS NMR spectrum from a fully hydrated zeolite sample. A 1.0 M aqueous solution of Al(NO3)3 was used as an external reference (0 ppm). The spectrum was normalized to 100 mg of the hydrated material.

[0048] The acidity of the sample was evaluated using acidity - pyridine adsorption. This study was conducted using a standard in - situ Fourier transform infrared (FTIR) setup. A 4 cm -1Using Nicolet Magna 550 FTIR spectroscopy equipped with a DTGS detector with an optical resolution of, the infrared spectrum was recorded using one level of zero filling for Fourier transformation. Before measurement, the sample was pulverized and pressed into a self-supporting disk (2 cm in diameter, approximately 5 mg / cm 2 ), and activated at 450 °C for 4 hours (2 °C / min) under vacuum (approximately 10 -6 hPa). After cooling to room temperature, the spectrum of the sample was recorded as a reference. Next, the saturation pressure (1 torr of pyridine) of the probe molecule was established in the cell at ambient temperature until saturation was reached. The wafer was heated at 150 °C for 30 minutes to promote the diffusion of the probe molecule into the sample. Continuous evacuation was performed at 15-minute intervals at room temperature, 150 °C, 200 °C, 250 °C, 300 °C, and 350 °C. All spectra were normalized to 20 mg of dehydrated zeolite. The amount of Lewis sites (L) and Bronsted (B) sites was determined using the band area of coordinated pyridine at 1450 cm -1 and the band area of adsorbed pyridine at 1545 cm -1 , respectively. The molar absorption coefficients (ε) used for quantification were obtained from Guisnet et al.: ε1545 (B-pyridine) = 1.13 cm / μmol and ε 1455 (L-pyridine) = 1.28 cm / μmol. The OMNIC version 7.3 SP1 program was used for data processing.

[0049] As used herein, the term "alpha value" means the catalytic activity of a material (e.g., the EWT framework zeolite described herein) measured by the ratio of the rate constant of a test sample for normal hexane to the rate constant of a reference catalyst, which may be amorphous silica / alumina in some cases. See, for example, P. B. Weisz and J. N. Miale, J. Catalysis, 4 (1965) 527-529; and J. N. Miale, N. Y. Chen, and P. B. Weisz, J. Catalysis, 6(1966) 278-287. For example, an alpha value of 1 means that the test sample and the reference material have approximately the same activity. In one or more embodiments, the treated EWT framework zeolite of the second aspect of the present invention may have an alpha value greater than 10. The micropore volume of the modified EWT framework zeolite described herein can be determined using methods known in the related art. For example, the material can be measured using physical adsorption of nitrogen, and the data can be analyzed by the t-plot method described in Lippens, B.C. et al., “Studies on pore system in catalysts: V. The t method”, J. Catal., 4, 319 (1965), which is hereby incorporated by reference for its description of the micropore volume method. Using such a physical adsorption method of nitrogen, the treated EWT framework zeolite of the second aspect of the present invention may have a micropore volume of 0.15 to 0.30, 0.25 to 0.30 cc / g, or 0.20 to 0.30 cc / g.

[0050] The X-ray diffraction data reported in this specification were collected by powder X-ray diffraction (PXRD) using a PANalytical X’Pert Pro diffractometer with average Cu Kα radiation (λ = 1.5418 Å). We used a θ-2θ scan in the 2θ range of 3 - 50° and a step of 0.02°. The instrument contribution to line broadening was calibrated based on the LaB6 srm660b standard powder from the National Institute of Standards and Technology. The interplanar spacing, d-spacing, was calculated in angstrom units. The relative intensity of the line I / I o is the ratio of the peak intensity to the intensity of the strongest line above the background. The intensity is not corrected for the Lorentz and polarization effects. The interplanar spacing, d-spacing, was calculated in angstrom units. The relative peak area intensity of the line I / I(o) is 1 / 100 of the intensity of the strongest line above the background and was determined using the MDI Jade peak profile fitting algorithm. It should be understood that the diffraction data presented as single lines can consist of multiple overlapping lines that may appear as split lines or partially split lines under certain conditions, such as differences in crystallographic changes. Typically, crystallographic changes can include minor changes in unit cell parameters and / or changes in crystal symmetry, rather than changes in structure. These minor effects, including changes in relative intensity, can result from differences in cation content, framework composition, nature and extent of pore filling, crystal size and shape, preferred orientation, and thermal and / or hydrothermal history.

[0051] Aspects of the present disclosure will be described in further detail using specific examples. The following examples are provided for illustrative purposes and are not intended to limit the present disclosure in any way. Those skilled in the relevant art will readily recognize various parameters that can be changed or modified to yield essentially the same results.

Examples

[0052] The following, Example 1 and Example 2 are reference examples disclosing the preparation of as-prepared EMM-23 and calcined EMM-23, respectively. Examples 3, 6, 7, 13, and 15 are reference examples disclosing single treatments of calcined EMM-23 using a solution containing an aluminum salt. Examples 4, 5, 14, and 16 are reference examples disclosing single treatments of as-prepared EMM-23 using a solution containing an aluminum salt. Examples 8-12 disclose repeated treatments of calcined EMM-23 using a solution containing an aluminum salt according to the present invention.

[0053] Example 1 - Hydrothermal Synthesis of As-Prepared EMM-23 37.3 g of a 15% aluminum nitrate solution was dissolved in 1211.5 g of 22.4 wt% 1,1-(pentane-1,5-diyl)bis(1-propylpyrrolidinium) hydroxide. 1.9 g of EMM-23 seeds were added to the aluminate solution and stirred until the seeds were well distributed. While stirring vigorously, 499.0 g of tetramethyl orthosilicate (TMOS) was slowly added to the seed-containing aluminate solution. The mixture was stirred for 30 minutes to completely hydrolyze the TMOS. To obtain an appropriate H2O / SiO2 ratio, the mass of the mixture was reduced to 765.3 g by heating at 75 °C in a forced-air drying oven. The mixture was transferred to a 2 L stirred autoclave. While stirring at 250 rpm, the mixture was heated to 150 °C. After reacting the slurry at 150 °C for 120 hours, the resulting crystalline product was separated from any liquid by vacuum filtration and washed three times with water of the reactor volume. After drying on a vacuum filter, the wet cake was dried at 120 °C for 16 hours to produce a dry cake. Powder XRD (see Figure 1) and elemental analysis by AA / ICP indicated that the resulting material was EMM-23 having an Si:Al2 ratio of approximately 400. Figure 2 shows the 27 Al MAS NMR spectrum of the as-prepared EMM-23 prepared in Example 1.

[0054] Example 2 - Calcination of As-Prepared EMM-23 from Example 1 A sample of as-prepared EMM-23 from Example 1 was heated in a muffle furnace from ambient temperature to 400 °C at a heating rate of 4 °C / min under a nitrogen flow of 100 cm 3 / min. Next, while raising the temperature to 540 °C using the same heating rate, nitrogen was gradually switched to air and maintained under an air flow at 540 °C for 2 hours. Figure 3 shows the powder XRD pattern of the calcined EMM-23 prepared in Example 2, and Figure 4 shows its 27 Al MAS NMR spectrum.

[0055] Example 3 - Treatment of Calcined EMM-23 with AlCl3·6H2O The following post-synthesis aluminization was performed on a sample of the calcined EMM-23 from Example 2. Post-synthesis aluminization was carried out using a 0.4 wt% AlCl3·6H2O solution at a solid:liquid ratio of 1:50. The mixture was stirred overnight at 80 °C with a stirring speed of 400 rpm. After treatment, the sample was purified by a series of high-speed centrifugation / decanting of the supernatant and redispersion of the sample under ultrasonic treatment (UT). This followed this protocol: 1) centrifugation / decanting at 20000 rpm for 20 minutes; 2) washing with water, redispersion under ultrasonic treatment (UT) for a duration of 10 minutes, centrifugation / decanting at 20000 rpm for 20 minutes; 3) washing with 0.1 M NH4OH, UT = 20 minutes, centrifugation / decanting at 20000 rpm for 20 minutes; and 4) washing 4 times with water, UT, and centrifugation / decanting at 20000 rpm for 20 minutes each time; Next, the treated EMM-23 was dried in an oven at 60 °C overnight. The powder XRD pattern is shown in Figure 5.

[0056] Example 4 - Treatment of As-Prepared EMM-23 with AlCl3·6H2O A sample of as-prepared EMM-23 prepared in Example 1 was subjected to the treatment described in Example 3. The powder XRD pattern is shown in Figure 6. Example 5 - Treatment of As-Prepared EMM-23 with AlCl3·6H2O and Water Washing The as-prepared EMM-23 sample of Example 1 was subjected to post-synthesis aluminization as described in Example 3. However, the sample was not washed with NH4OH. Instead, to make the number of washing steps the same as that in Example 3, the sample was washed 6 times with only H2O. The obtained sample was then dried overnight in an oven at 60 °C. The powder XRD pattern is shown in Figure 7.

[0057] Example 6 - Treatment of calcined EMM-23 with AlCl3·6H2O and water washing The calcined EMM-23 sample of Example 2 was subjected to post-synthesis aluminization as described in Example 3. However, the sample was not washed with NH4OH. Instead, to make the number of washing steps the same as that in Example 3, the sample was washed 6 times with only H2O. The obtained sample was then dried overnight in an oven at 60 °C. The powder XRD pattern is shown in Figure 8.

[0058] Example 7 - Treatment of calcined EMM-23 with AlCl3·6H2O The calcined EMM-23 sample prepared in Example 2 was subjected to the following post-synthesis aluminization treatment. This treatment was carried out using a 0.4 wt% AlCl3·6H2O solution at a solid:liquid ratio of 1:50. The mixture was stirred at 80 °C for 3 hours at a stirring speed of 400 rpm. After treatment, the sample was purified by a series of 3 steps of high-speed centrifugation / decanting of the supernatant and redispersion of the sample in water under ultrasonic treatment (15 minutes each time). The treated EMM-23 was then dried overnight in an oven at 60 °C. The powder XRD pattern is shown in Figure 9.

[0059] Examples 8 to 12 - Repeated treatment of calcined EMM-23 with AlCl3·6H2O In Example 8, a sample of the treated EMM-23 prepared in Example 7 was subjected to the same treatment as described in Example 7 for the second time. In Example 9, a sample of the treated EMM-23 prepared in Example 8 was subjected to the same treatment as described in Example 7 for the third time. In Example 10, a sample of the treated EMM-23 prepared in Example 9 was subjected to the same treatment as described in Example 7 for the fourth time. In Example 11, a sample of the treated EMM-23 prepared in Example 10 was subjected to the same treatment as described in Example 7 for the fifth time. In Example 12, a sample of the treated EMM-23 prepared in Example 11 was subjected to the same treatment as described in Example 7 for the sixth time. Figure 10 shows the 27 Al MAS NMR spectra of the calcined EMM-23 prepared in Example 2 and the treated EMM-23 of Examples 7 to 12 (*the small peaks marked are spinning sidebands).

[0060] Example 13 - Treatment of Calcined EMM-23 with AlNO3·9H2O The following post-synthesis aluminization treatment was performed on a sample of the calcined EMM-23 prepared in Example 2. This treatment was carried out using a 0.25 M AlNO3·9H2O solution at a solid:liquid ratio of 1:50. The mixture was stirred at 80 °C overnight at a stirring speed of 400 rpm. After treatment, the sample was purified by a series of six high-speed centrifugations / decanting of the supernatant and redispersion of the sample in water under ultrasonic treatment (15 minutes each time). The treated EMM-23 was then dried in an oven at 60 °C overnight. Example 14 - Treatment of As-Prepared EMM-23 with AlNO3·9H2O A sample of the as-prepared EMM-23 prepared in Example 1 was subjected to the aluminization treatment described in Example 13.

[0061] Example 15 - Treatment of Calcined EMM-23 with (NH4)3AlF6 A sample of calcined EMM-23 prepared in Example 2 was subjected to the following post-synthesis aluminization treatment. This treatment was carried out using a 0.02 M (NH4)3AlF6 solution at a solid:liquid ratio of 1:30. The mixture was stirred overnight at 25 °C with a stirring speed of 400 rpm. After the treatment, the sample was purified by a series of three-step high-speed centrifugation / decanting of the supernatant and redispersion of the sample in hot water under ultrasonic treatment (15 minutes each time). The obtained treated EMM-23 was then dried overnight in an oven at 60 °C. Example 16 - Treatment of as-prepared EMM-23 with (NH4)3AlF6 A sample of as-prepared EMM-23 prepared in Example 1 was subjected to the following post-synthesis aluminization treatment. This treatment was carried out using a 0.02 M (NH4)3AlF6 solution at a solid:liquid ratio of 1:30. The mixture was stirred for 30 minutes at RT under ultrasonic treatment. After the treatment, the sample was purified by a series of three-step high-speed centrifugation / decanting of the supernatant and redispersion of the sample in hot water under ultrasonic treatment (15 minutes each time). The obtained treated EMM-23 was then dried overnight in an oven at 60 °C.

[0062] Discussion The Si:Al2 ratios and Brønsted acidities of the materials obtained in Examples 1 - 16 are shown in Table 7 below.

[0063] Table 7

Table 7

[0064] The results in Table 7 reveal that the calcined EMM-23 zeolite prepared in Example 2 had an Si:Al2 ratio of 375. This suggests that extremely little Al was incorporated into the zeolite during crystallization. Example 3 shows that overnight treatment of the zeolite with an aluminum salt solution resulted in an increase in the amount of Al in the zeolite, and as a result, the Si:Al2 ratio decreased to 60. Example 6 reveals similar results. Example 7 shows that a single 3-hour treatment can also increase the Al concentration in the zeolite, but not to the same extent as the overnight treatment in Example 3.

[0065] Examples 8 - 12 show that repeated treatments result in a gradual increase in the Al concentration in the zeolite, but the degree of increase with each treatment generally decreases as the number of repetitions n progresses from n = 2 (Example 8) to n = 6 (Example 12). Surprisingly, even with a total treatment time of only 6 hours (n = 2, Example 8), the Si:Al2 ratio is already lower than that of the longer overnight treatments in Examples 3 and 6. Examples 3, 6, and 7 - 12 show the treatment of the zeolite with AlCl3·6H2O. Examples 14 and 16 show the treatment of the zeolite with AlNO3·9H2O and (NH4)3AlF6, respectively. Examples 4 and 5 show that treatment with an aluminum chloride solution is also effective in increasing the aluminum content of the as-prepared zeolite. Examples 14 and 16 show the treatment of the as-prepared zeolite with AlNO3·9H2O and (NH4)3AlF6, respectively.

[0066] Figure 11A shows the overlay powder XRD patterns of the calcined EMM-23 prepared in Examples 2, 3, 6 - 13, and 15. Figure 11B shows the overlay powder XRD patterns of the as-prepared EM-23 prepared in Examples 1, 4, 5, 14, and 16. From the foregoing description, various modifications of the present disclosure will be apparent to those skilled in the art in addition to what is described herein. Such modifications are also intended to fall within the scope of the appended claims. Without limitation, all patents, patent applications, and publications cited in this application, including all references, are hereby incorporated by reference in their entirety.

[0067] Furthermore, alternatively or in addition, the present invention relates to the following embodiments. Embodiment 1: A process for increasing the aluminum content of an EWT framework zeolite and mixtures thereof, the process comprising subjecting the EWT framework zeolite to the following steps: a) contacting the EWT framework zeolite with an aqueous aluminum salt solution; and b) separating the EWT framework zeolite from the aqueous aluminum salt solution wherein the treatment comprises and repeating this treatment such that the EWT framework zeolite undergoes a total of n treatment cycles, where n is a number in the range of 2 to 10. Embodiment 2: The process of Embodiment 1, wherein in step a), the EWT framework zeolite is contacted with the aqueous aluminum salt solution for a duration in the range of 1 hour to 24 hours. Embodiment 3: The process of Embodiment 1 or 2, wherein the aluminum salt is selected from the group consisting of Al2(SO4)3, AlCl3, Al(NO3)3, (NH4)3AlF6, and mixtures thereof. Embodiment 4: The process according to any one of Embodiments 1 to 3, wherein in one or more treatment cycles, after step b), step c) of contacting the EWT framework zeolite with a washing liquid is also included. Embodiment 5: The process of Embodiment 4, wherein in at least one treatment cycle, the washing liquid is water. Embodiment 6: The process of Embodiment 4 or 5, wherein in at least one treatment cycle, the washing liquid is an aqueous ammonium hydroxide solution. Embodiment 7: A process according to any one of Embodiments 1 to 6, including, in one or more processing cycles, after step b) or, if it exists, after step c), step d) of drying the EWT framework zeolite. Embodiment 8: A process according to any one of Embodiments 1 to 7, wherein the contacting step is carried out at a temperature in the range of 50°C to 100°C during step a). Embodiment 9: A process according to any one of Embodiments 1 to 8, wherein n is 3 to 6. Embodiment 10: A process according to any one of Embodiments 1 to 9, wherein the EWT framework zeolite is a calcined EWT framework zeolite. Embodiment 11: A process according to any one of Embodiments 1 to 10, wherein the EWT framework zeolite is an uncalcined EWT framework zeolite. Embodiment 12: A process according to any one of Embodiments 1 to 11, wherein the EWT framework zeolite is EMM-23. Embodiment 13: A process according to any one of Embodiments 1 to 12, wherein the EWT framework zeolite is in the form of non-bonded zeolite crystals. Embodiment 14: An EWT framework zeolite produced by a process according to any one of the preceding embodiments, wherein the ratio Si:Al2 is 70 or less.

[0068] Embodiment 15: A process for converting an organic compound into a conversion product, the process comprising contacting the organic compound with the EWT framework zeolite of Embodiment 14.

Claims

1. A process for increasing the aluminum content of EWT skeleton zeolite and mixtures thereof, wherein the EWT skeleton zeolite is subjected to the following steps: a) The step of contacting the EWT skeleton zeolite with an aluminum salt aqueous solution; and b) Separating the EWT skeleton zeolite from the aluminum salt aqueous solution. The process includes the following: The process further includes repeating the process such that the EWT skeleton zeolite undergoes a total of n processing cycles, where n is a number in the range of 2 to 10.

2. The process according to claim 1, wherein in step a), the EWT skeleton zeolite is in contact with the aluminum salt aqueous solution for a duration ranging from 1 hour to 24 hours.

3. The aluminum salt is Al 2 (SO 4 ) 3 , AlCl 3 , Al(NO 3 ) 3 , (NH 4 ) 3 AlF 6 and a mixture thereof, the process according to claim 1.

4. In one or more processing cycles, the processing occurs after step b), c) The step of washing the EWT skeleton zeolite with a washing solution, The process according to claim 1.

5. The process according to claim 4, wherein the cleaning solution is water in at least one processing cycle.

6. The process according to claim 4, wherein in at least one processing cycle, the cleaning solution is an aqueous solution of ammonium hydroxide.

7. In one or more processing cycles, the processing occurs after step b), or after step c) if present. d) The step of drying the EWT skeleton zeolite, The process according to claim 1.

8. During step a), the contact step is performed at a temperature in the range of 50°C to 100°C. The process according to claim 1.

9. The process according to claim 1, wherein n is 3 to 6.

10. The process according to claim 1, wherein the EWT skeleton zeolite is calcined EWT skeleton zeolite.

11. The process according to claim 1, wherein the EWT skeleton zeolite is an uncalcined EWT skeleton zeolite.

12. The process according to claim 1, wherein the EWT skeleton zeolite is EMM-23.

13. The process according to claim 1, wherein the EWT skeleton zeolite is in the form of an unbonded zeolite crystal.

14. Ratio Si:Al 2 EWT skeleton zeolite produced by the process according to any one of claims 1 to 13, wherein the ratio is 70 or less.

15. A process for converting an organic compound into a conversion product, comprising the step of contacting the organic compound with the EWT skeleton zeolite described in claim 14.

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