DEHYDROXYLATION PRETREATMENT OF INORGANIC MATERIALS IN MESOPORE INTRODUCTION PROCESS

Abstract

Mesoporous compositions and methods for preparing mesoporous and/or mesostructured materials from inorganic materials are provided. Various embodiments described herein relate to the preparation of mesoporous and/or mesostructured zeolites via a dehydroxylation pretreatment followed by a mesopore introduction step.

Description

BACKGROUND

1. Field of the Invention

Various embodiments of the present invention relate generally to pretreatment of inorganic materials prior to mesopore introduction treatment. More particularly, various embodiments relate to methods for dehydroxylating inorganic materials prior to mesopore introduction treatment.

2. Description of the Related Art

Zeolites and related crystalline molecular sieves are widely used due to their regular microporous structure, strong acidity, and ion-exchange capability. However, their applications are limited by their small pore openings, which are typically narrower than 1 nm. The discovery of MCM-41, with tuneable mesopores of 2 to 10 nm, overcomes some of the limitations associated with zeolites. However, unlike zeolites, MCM-41-type materials are not crystalline, and do not possess strong acidity, high hydrothermal stability, and high ion-exchange capability.

Over the past 10 years, a great deal of effort has been devoted to understanding and improving the structural characteristics of MCM-41. It was found that the properties of Al-MCM-41 could be improved through (1) surface silylation, (2) Al grafting on the pore walls to increase acidity, (3) salt addition during synthesis to facilitate the condensation of aluminosilicate groups, (4) use of organics typically employed in zeolite synthesis to transform partially the MCM-41 wall to zeolite-like structures, (5) preparation of zeolite/MCM-41 composites, (6) substitution of cationic surfactants by tri-block copolymers and Gemini amine surfactants to thicken the walls, and (7) assembly of zeolite nanocrystals into an ordered mesoporous structure. In the latter approach, the first steam-stable hexagonal aluminosilicate (named MSU-S) was prepared using zeolite Y nanoclusters as building blocks. Pentasil zeolite nanoclusters were also used to produce MSU-S_(MFI) and MSU-S_(BEA),

FIG. 1 a is a schematic illustration of a prior art amorphous mesoporous material 100. As shown in FIG. 1a, zeolite nuclei 105a, 105b, 105c were aggregated around surfactant micelles under controlled conditions to form a solid. Thereafter, the aggregated nuclei 105a, 105b, 105c were washed in water and dried and the surfactant was extracted to provide a desired mesopore-sized pore volume 110, forming amorphous mesoporous zeolite nuclei material 100. Each of the zeolite nuclei, for example, 105a, 105b, 105c, is a nanosized crystal. When they are aggregated, the material 100 is polycrystalline because the nuclei material is lacking the long-range regular lattice structure of the crystalline state (i.e., the aggregated nuclei are not fully crystalline or truly crystalline).

Some strategies have managed to improve appreciably the acidic properties of Al-MCM-41 materials. However, due to the lack of long-range crystallinity in these materials, their acidity is not as strong as those exhibited by zeolites. For example, semicrystalline mesoporous materials, such as nanocrystalline aluminosilicate PNAs and Al-MSU-S_(MFI), being even more active than conventional Al-MCM-41, showed significantly lower activity than H-ZSM-5 for cumene cracking; the catalyst activity for this reaction has usually been correlated to the Bronsted acid strength of the catalyst.

Previous attempts to prepare mesostructured zeolitic materials have been ineffective, resulting in separate zeolitic and amorphous mesoporous phases. Moreover, some authors have pointed out the difficulty of synthesizing thin-walled mesoporous materials, such as MCM-41, with zeolitic structure, due to the surface tension associated with the high curvature of the mesostructure.

SUMMARY OF THE INVENTION

One embodiment of the invention concerns a method of preparing a mesoporous inorganic material, the method comprising: (a) treating at least one initial inorganic material for a period of time in a dehydroxylation environment to thereby produce a dehydroxylated inorganic material; and (b) contacting the dehydroxylated inorganic material with at least one pH controlling agent to thereby produce the mesoporous inorganic material.

Another embodiment of the invention concerns a method of preparing a mesoporous zeolite, the method comprising: (a) treating at least one zeolite for a period of time in a heat-treating environment having a temperature of at least 500° C. to thereby produce a heat-treated zeolite, wherein the heat-treating environment primarily comprises air and/or an inert gas in addition to the zeolite; and (b) contacting the heat-treated zeolite with at least one pH controlling agent to thereby produce said mesoporous zeolite.

Yet another embodiment of the invention concerns a method of preparing a mesoporous zeolite, the method comprising: (a) contacting at least one zeolite with steam having a temperature of at least 300° C. for a period of time to thereby produce a steam-treated zeolite; and (b) contacting the steam-treated zeolite with at least one pH controlling agent to thereby produce said mesoporous zeolite.

Still another embodiment of the invention concerns a method of preparing a mesoporous zeolite having a target mesopore volume, the method comprising: (a) setting a total mesopore volume target; (b) treating a first zeolite under first dehydroxylation conditions in a dehydroxylation environment to thereby produce a first dehydroxylated zeolite; (c) treating the first dehydroxylated zeolite under first mesopore forming conditions to thereby produce a first mesoporous zeolite, wherein the first mesopore forming conditions comprise contacting the first dehydroxylated zeolite with at least one pH controlling agent; (d) measuring the mesopore volume of the first mesoporous zeolite and comparing the mesopore volume of the first mesoporous zeolite to the total mesopore volume target of step (a); (e) treating a second zeolite under second dehydroxylation conditions in the dehydroxylation environment to thereby produce a second dehydroxylated zeolite; and (f) treating the second dehydroxylated zeolite under second mesopore forming conditions to thereby produce a second mesoporous zeolite, wherein the second mesopore forming conditions comprise contacting the second dehydroxylated zeolite with at least one pH controlling agent, wherein the second dehydroxylation conditions and/or the second mesopore forming conditions are adjusted in relation to the first dehydroxylation conditions and/or the first mesopore forming conditions according to the results of the comparison of step (d).

BRIEF DESCRIPTION OF THE DRAWINGS

Embodiments of the invention are described in detail below with reference to the attached drawing figures, wherein:

FIG. 1 a is a schematic diagram of a prior art polycrystalline mesoporous material;

FIG. 1 b is a schematic illustration of a fully crystalline mesostructured zeolite;

FIG. 1 c depicts a transmission electron microscopy (“TEM”) image of a nanostructured zeolite where the nanostructure shape includes nanorods;

FIG. 1 d depicts the X-ray diffraction (“XRD”) pattern of a fully crystalline mesostructured zeolite H—Y[MCM-41]. Both the ordered mesostructure MCM-41 (revealed by the XRD peaks at low angles) and the unmodified zeolitic fully crystalline structure H—Y are present;

FIG. 2 depicts the X-ray diffraction pattern of the fully crystalline mesostructured zeolite H-MOR[MCM-41]. Both the ordered mesostructure MCM-41 (revealed by the XRD peaks at low angles) and the unmodified zeolitic fully crystalline structure H-MOR are present;

FIG. 3 depicts the X-ray diffraction pattern of the fully crystalline mesostructured zeolite H-ZSM-5[MCM-41]. Both the ordered mesostructure MCM-41 (revealed by the XRD peaks at low angles) and the unmodified zeolitic crystalline structure H-ZSM-5 are present;

FIG. 4 depicts Fourier transform infrared spectroscopy (“FTIR”) characterization peaks for the fully crystalline mesostructured zeolite H—Y[MCM-41], labeled Meso-H—Y, and the unmodified zeolite Y;

FIG. 5 depicts FTIR spectra of fully crystalline mesostructured zeolites H—Y[MCM-41] (upper top), H-MOR[MCM-41] (upper middle), and H-ZSM-5[MCM-41] (upper bottom); and FTIR spectra of their unmodified fully crystalline zeolitic versions H—Y (lower top), H-MOR (lower middle), and H-ZSM-5 (lower bottom). A match between each fully crystalline mesostructured zeolite and its corresponding unmodified zeolite is observed, indicating the fully zeolitic connectivity present in the fully crystalline mesostructured zeolites;

FIG. 6 depicts the physisorption isotherm of N₂ at 77 K of a fully crystalline mesostructured zeolite H—Y[MCM-41], labeled Meso-HY, and its unmodified zeolitic version, H—Y. The pore size distribution (Barrett, Joyner, Halenda (“BJH”) method) of the fully crystalline mesostructured zeolite is included in the inset. The presence of well developed narrow pore size mesoporosity in the mesostructured sample is evident by the sharp uptake at P/P₀˜0.3;

FIG. 7 depicts the physisorption isotherm of N₂ at 77 K of a fully crystalline mesostructured zeolite H-MOR[MCM-41], labeled Meso-HMOR, and its unmodified zeolitic version, H-MOR. The pore size distribution (BJH method) of the fully crystalline mesostructured zeolite is included in the inset. The presence of well developed narrow pore size mesoporosity in the mesostructured sample is evident by the sharp uptake at P/P₀˜0.3;

FIG. 8 depicts the physisorption isotherm of N₂ at 77 K of a fully crystalline mesostructured H-ZSM-5[MCM-41], labeled Meso-HZSM5, and its unmodified zeolitic version, HZSM5. The pore size distribution (BJH method) of the fully crystalline mesostructured zeolite is included in the inset. The presence of well developed narrow pore size mesoporosity in the mesostructured sample is evident by the sharp uptake at P/P₀˜0.3;

FIG. 9 depicts pore volumes (darker columns) of fully crystalline mesostructured zeolites H—Y[MCM-41] (left), H-MOR[MCM-41] (center), and H-ZSM-5[MCM-41] (right) and their unmodified zeolitic versions (lighter columns) of H—Y (left), H-MOR (center), and H-ZSM-5 (right);

FIG. 10 a depicts images obtained by TEM of detail of an H—Y[MCM-41] fully crystalline mesostructured zeolite. The electron diffraction pattern is included as an inset;

FIG. 10 b depicts images obtained by TEM of detail of an H—Y[MCM-41] fully crystalline mesostructured zeolite at different focus. The electron diffraction pattern is included as an inset;

FIG. 11 depicts a TEM image of a fully crystalline mesostructured zeolite;

FIG. 12 depicts a TEM image of a fully crystalline mesostructured zeolite;

FIG. 13 depicts a schematic illustration of catalytic cracking of 1,3,5-triisopropyl benzene by an unmodified conventional zeolite H—Y;

FIG. 14 depicts a schematic illustration of catalytic cracking of 1,3,5-triisopropyl benzene by a fully crystalline mesostructured zeolite;

FIG. 15 depicts catalytic activity for 1,3,5-triisopropyl benzene cracking shown as conversion vs. time for a fully crystalline mesostructured zeolite H—Y[MCM-41], labeled Meso-HY, its unmodified zeolitic version HY, and a conventional AlMCM-41. A 50 mL/min stream of He saturated with 1,3,5-triisopropylbenzene at 120° C. was flowed at 200° C. over 50 mg of catalyst;

FIG. 16 depicts the catalytic cracking of 1,3,5-triisopropyl benzene with a fully crystalline mesostructured zeolite H—Y[MCM-41], labeled Meso-HY, to diisopropyl benzene and cumene. The H—Y[MCM-41] results are compared to the normalized results from a commercial sample of unmodified fully crystalline zeolite H—Y. Catalytic cracking with the fully crystalline mesostructured zeolite H—Y[MCM-41] results in higher selectivity and reduction in benzene production;

FIG. 17 depicts the hydrothermal stability of the fully crystalline mesostructured zeolite H—Y, H—Y[MCM-41], labeled Meso-HY, compared to the conventional non-mesolytic zeolite Al-MCM-41;

FIG. 18 depicts catalytic activity for 1,3,5-triisopropyl benzene cracking shown as conversion vs. time for a fully crystalline mesostructured zeolite H-MOR[MCM-48], labeled Meso-HMOR, and its unmodified zeolitic version H-MOR. A helium flow of 50 mL/min saturated with 1,3,5-triisopropylbenzene at 120° C. was introduced over 50 mg of each catalyst, H-MOR[MCM-48] and H-MOR, at 200° C.;

FIG. 19 depicts catalytic activity for 1,3,5-triisopropyl benzene cracking shown as conversion vs. time for a fully crystalline mesostructured zeolite H-ZSM-5[MCM-41], labeled Meso-H-ZSM-5, and its unmodified zeolitic version H-ZSM-5. A helium flow of 50 mL/min saturated with 1,3,5-triisopropylbenzene at 120° C. was introduced over 50 mg of each catalyst, H-ZSM-5[MCM-41] and H-ZSM-5, at 200° C.;

FIG. 20 a depicts, on the left-hand side Y axis, the conversion of 1,3,5-triisopropylbenzene vs. time for the nanostructure H-MOR[ZNR] and the unmodified fully crystalline zeolite H-MOR. The ratio of benzene produced by H-MOR-to-benzene produced by H-MOR[ZNR] as a function of time is shown on the right-hand side Y axis. A helium flow of 50 mL/min saturated with 1,3,5-triisopropylbenzene at 120° C. was introduced over 50 mg of each catalyst, H-MOR[ZNR] and H-MOR, at 200° C.;

FIG. 20 b depicts Microactivity test (“MAT”) results of a conventional fully crystalline zeolite HY (Si/Al=15) and its fully crystalline mesostructured version HY[MCM-41];

FIG. 20 c depicts the composition of the LPG fraction obtained by MAT of a conventional fully crystalline zeolite HY (Si/Al=15) and its fully crystalline mesostructured version HY[MCM-41];

FIG. 21 depicts the percentage of polyethylene (“PE”) weight lost vs. temperature for the mixtures of catalysts in weight ratio to PE labeled: (A): no catalyst; (B): H-ZSM-5:PE, 1:2; (C): H-ZSM-5[MCM-41]:PE, 1:2; (D): H-ZSM-5:PE, 1:1; (E) H-ZSM-5:PE, 2:1; (F): H-ZSM-5[MCM-41]:PE, 1:1; and (G) H-ZSM-5[MCM-41]:PE, 2:1;

FIG. 22 depicts the FTIR spectra of a) H—Y[MCM-41], b) NH₄—Y[MCM-41], c) NH₂(CH₂)₂NMe₃Cl, d) NH₂(CH₂)₂NMe₃-Y[MCM-41], d) Rh(PPh₃)₃Cl, and e) Rh(PPh₃)₃NH₂(CH₂)₂NMe₃-Y[MCM-41]; and

FIG. 23 depicts MAT yield results where a fully crystalline mesostructured zeolite HY[MCM-41] is employed as an additive to a conventional unmodified zeolite HY for fluid catalytic cracking of a vacuum gas oil. The results from left to right on the X-axis show 100% HY with no additive, 10% HY[MCM-41] additive to the catalyst, 20% HY[MCM-41] additive to the catalyst, 50% HY[MCM-41] additive to the catalyst, and 100% HY[MCM-41].

DETAILED DESCRIPTION

Various embodiments of the present invention relate to a method of enhancing the mesoporosity of inorganic materials having long-range crystallinity. Such inorganic materials can by prepared by treating an initial inorganic material with a pH controlling agent and, optionally, a surfactant under time and temperature conditions. In one or more embodiments, the initial inorganic material can undergo dehydroxylation pretreatment prior to mesopore introduction. The resulting inorganic material with enhanced mesoporosity can have one or more of a variety of mesostructures. Following formation, in various embodiments, the mesostructured inorganic materials having enhanced mesoporosity can be variously modified and/or employed in a variety of processes.

Initial Inorganic Material

As noted above, an initial inorganic material can be employed in forming the inorganic materials having long-range crystallinity and enhanced mesoporosity. In various embodiments, the initial inorganic material can have a 1-dimensional, 2-dimensional, or 3-dimensional pore structure. Additionally, the initial inorganic material can itself exhibit long-range crystallinity. Materials with long-range crystallinity include all solids with one or more phases having repeating structures, referred to as unit cells, that repeat in a space for at least 10 nm. A long-range crystalline inorganic material structure may have, for example, single crystallinity, mono crystallinity, or multi crystallinity. Multi crystalline materials include all solids having more than one phase having unit cells that repeat in a space for at least 10 nm. Furthermore, in various embodiments, the initial inorganic material can be fully crystalline. Additionally, the initial inorganic material can be a one-phase hybrid material. Examples of inorganic materials suitable for use as the initial inorganic material include, but are not limited to, metal oxides, zeolites, zeotypes, aluminophosphates, silico-aluminophosphates, gallophosphates, zincophosphates, and titanophosphates. Combinations of two or more types of these inorganic materials can also be employed as the initial inorganic material. In addition, the inorganic material can be a zeolite-like material, which represents a growing family of inorganic and organic/inorganic molecular sieves. In one or more embodiments, the initial inorganic material comprises a zeolite. Examples of zeolites suitable for use as the initial inorganic material include, but are not limited to, faujasite (i.e., zeolite Y; “FAU”), mordenite (“MOR”), ZSM-5 (“MFI”), and CHA. Additionally, ultra-stable (e.g., zeolite USY) and/or acid forms of zeolites can also be employed. In various embodiments, the initial inorganic material can comprise faujasite, mordenite, ZSM-5, or mixtures of two or more thereof. In certain embodiments, the zeolite is selected from the group consisting of ZSM-5, ZSM-12, ZSM-22, beta zeolite, synthetic ferrierite (ZSM-35), synthetic mordenite, and mixtures of two or more thereof. In a particular embodiment, the zeolite comprises ZSM-5.

In certain embodiments, the initial inorganic material can have a low silica-to-alumina ratio (i.e., SiO₂/Al₂O₃). For example, the initial inorganic material can have a silica-to-alumina ratio of at least 10, 15, or 20. Additionally or alternatively, the initial inorganic material can have a silica-to-alumina ratio in the range from about 10 to about 1,000, about 10 to about 500, about 10 to about 250, about 15 to about 150, about 15 to about 100, about 15 to about 75, or about 20 to about 30. Generally, the SiO₂/Al₂O₃ of an initial inorganic material can be determined via bulk chemical analysis. In various embodiments described herein, the silica-to-alumina ratio can be determined by known methods in the art.

In one or more embodiments, the initial inorganic material can be present as a part of a composite shaped article comprising at least one inorganic material (e.g., a zeolite) and at least one non-zeolitic material. In one or more embodiments, the inorganic material in the composite shaped article can be a zeolite as described above. The composite shaped article can comprise the inorganic material (e.g., a zeolite) in an amount of at least 0.1 weight percent, at least 15 weight percent, or at least 30 weight percent based on the total weight of the composite shaped article. Furthermore, the composite shaped article can comprise the inorganic material (e.g., a zeolite) in an amount in the range of from about 0.1 to about 99 weight percent, in the range of from about 5 to about 95 weight percent, in the range of from about 15 to about 70 weight percent, or in the range of from 30 to 65 weight percent based on the total weight of the composite shaped article.

In various embodiments, the non-zeolitic material of the composite shaped article can comprise one or more components selected from the group consisting of inert stable oxides, inert stable carbides, inert stable nitrides, and mixtures of two or more thereof. Examples of inert stable oxides suitable for use include, but are not limited to, alpha-aluminum oxide, titanium dioxide, zirconium oxide, mullite, hydrous kaolin clay, and the residue of alkaline extraction of kaolin clay which has been calcined through the characteristic exotherm at about 1,780° F. without substantial formation of mullite. An example of an inert stable carbide includes, but is not limited to, silicon carbide. An example of an inert stable nitride includes, but is not limited to, silicon nitride. In other various embodiments, the non-zeolitic material of the composite shaped article can comprise a substantially insoluble alkaline oxide, such as, for example, magnesium oxide or calcium oxide. In one or more embodiments, the composite shaped article can have a total non-zeolitic material content of at least 15, at least 30, or at least 35 weight percent based on the total weight of the composite shaped article. Furthermore, the composite shaped article can have a total non-zeolitic material content in the range of from about 1 to about 99.9 weight percent, in the range of from about 5 to about 95 weight percent, in the range of from about 30 to about 85 weight percent, or in the range of from 35 to 70 weight percent based on the total weight of the composite shaped article.

The composite shaped article can be formed by a variety of methods. In various embodiments, the composite shaped article can be formed by first combining the non-zeolitic material with at least one zeolitic material to form an initial mixture. The zeolitic and non-zeolitic materials can be present in the initial mixture in amounts described above for the composite shaped article. Thereafter, the initial mixture can be shaped into the composite shaped article.

Alternatively, the composite shaped article can be prepared by (i) combining the non-zeolitic material and/or a precursor of the non-zeolitic material with a zeolite precursor to form an initial mixture; (ii) shaping the initial mixture into an initial composite shaped article; and (iii) converting at least a portion of the zeolitic precursor in the initial composite shaped article into a zeolite thereby forming the composite shaped article. Suitable zeolite precursors include, but are not limited to, hydrous kaolin clay, metakaolin, sodium silicate, and sodium aluminate, any of which or a combination thereof may be employed in forming the initial mixture of step (i). After shaping the initial mixture, the initial composite shaped article can be treated under any conditions suitable for converting at least a portion of the zeolite precursors into zeolitic material. For example, the initial composite shaped article can be calcined at temperatures ranging from about 1,000 to about 1,400° F., or from 1,100 to 1,300° F. In various embodiments, the calcined material can be combined with additional zeolite precursors in a basic solution (e.g., a sodium hydroxide solution). The resulting mixture can be heated (e.g., from 100 to 300° F., or about 210° F.) while stirring for a time period in the range of from about 1 hour to about 1 week, in the range of from 12 hours to 2 days, or about 24 hours. Thereafter, the material can be filtered, washed with deionized water, and dried (e.g., at about 80° C.).

Regardless of the method employed, the initial mixture can be shaped into any desired shape suitable for the intended use of the final product. In various embodiments, the composite shaped article can have a shape selected from the group consisting of a pellet, a tablet, a microsphere, a bead, a honeycomb shape, or mixtures of two or more thereof. Any method known or hereafter discovered in the art can be employed for shaping the initial mixture. For example, the mixture can be shaped by extruding, molding, spray drying, pelletizing, or combinations thereof. In one or more embodiments, microspheres can be formed by spray drying the initial mixture. Once the material is shaped, it can be aged by, for example, being treated in air at a temperature ranging from, for example, about 10 to about 200° C. The shaped material can be treated for a time ranging from about 1 hour to about 1 week. Optionally, it can be heat treated a second time at a higher temperature. The second temperature can vary from about 200 to about 800° C. and for a time period from about 1 hour to about 1 week.

In various embodiments, the composite shaped article can be a Fluid Catalytic Cracking (“FCC”) catalyst. As known to those of ordinary skill in the art, FCC catalysts typically contain a molecular sieve (e.g., a zeolite such as faujasite), a binder, a filler, and a matrix. Thus, in various embodiments, the composite shaped article can contain various other components known or hereafter discovered by those skilled in the art of FCC catalysis. FCC catalysts suitable for use as the composite shaped article include any known or hereafter discovered FCC catalysts. In various embodiments, the FCC catalyst can be a faujasite-containing catalyst.

Pretreatments to the Initial Inorganic Material

In various embodiments, the initial inorganic material can be pretreated to alter a portion of the chemical structure of the initial inorganic material prior to mesopore introduction. The initial inorganic material can be subjected to a form of pretreatment including, for example, dehydroxylation, acid treatment, and combinations thereof.

In certain embodiments, the initial inorganic material can be subjected to dehydroxylation to form a partially-dehydroxylated inorganic material, a substantially completely dehydroxylated inorganic material, or a completely dehydroxylated inorganic material. In such embodiments, the dehydroxylation is capable of removing at least 10 percent, 15 percent, 20 percent, 30 percent, at least 50 percent, at least 60 percent, at least 70 percent, at least 80 percent, at least 90 percent, at least 95 percent, at least 99 percent, substantially all, or all of the acidic hydroxyl groups from the initial inorganic material.

In one or more embodiments, dehydroxylation can comprise subjecting at least a portion of the initial inorganic material to calcination, heat treatment, steam treatment, and combinations thereof. In certain embodiments, the dehydroxylation comprises subjecting the initial inorganic material to calcination and/or heat treatment, but does not include steam treatment. In alternative embodiments, the dehydroxylation comprises subjecting the initial inorganic material to steam treatment only and does not include calcination or heat treatment.

The dehydroxylation can occur at a temperature of at least 300° C., at least 400° C., at least 500° C., at least 600° C., at least 700° C., at least 800° C., at least 900° C., or at least 1,000 ° C. Additionally, the initial inorganic material can be dehydroxylated at a temperature in the range of from about 500 to about 1,200° C., in the range of from about 600 to about 1,200° C., in the range of from about 700 to about 1,000° C., or in the range of 800 to 1,000° C. Additionally or alternatively, the dehydroxylation can occur for a time period of at least 1 minute, 5 minutes, 10 minutes, 20 minutes, 30 minutes, 60 minutes, 5 hours, or 10 hours.

In various embodiments, dehydroxylation can be performed in a dehydroxylation environment comprising the initial inorganic material and further comprising air and/or an inert gas. In one embodiment, the air and/or inert gas are dried. In such embodiments, the dehydroxylation environment comprises no more than 90, 60, 50, 40, 30, 20, 15, 10, 5, 1, or 0.01 percent by volume of water. In an alternative embodiment, the air and/or the inert gas are not dried. In such embodiments, the dehydroxylation environment can comprise at least 0.01, 0.1, 1, 5, 10, 20, 30, 40, 50, 60, 70, 80, 90, 95, or 99 percent by volume of water. In another embodiment, the air and/or the inert gas are flowing. In an alternative embodiment, the air and/or the inert gas are stationary. In yet another embodiment, the inert gas comprises nitrogen. In still yet another embodiment, the dehydroxylation environment comprises dried, flowing air in addition to the inorganic material. In a particular embodiment, the dehydroxylation environment primarily comprises air in addition to the initial inorganic material. As used herein, “primarily” means that the air and/or inert gas comprise at least 50% by volume of the dehydroxylation environment. In such an embodiment, the dehydroxylation environment comprises air in an amount of at least 70, 80, 90, or 99 volume percent. In additional embodiments, the dehydroxylation environment can further comprise steam. In such embodiments, the steam can have a temperature of at least about 400, 500, 550, or 600° C. and/or not more than 1,000, 950, 900, 850, or 800° C.

In certain embodiments, the initial inorganic material can be initially treated with an acid. For instance, very stable zeolites having dense structures (e.g., ZSM-5) may benefit from pretreatment with acid. In one or more embodiments, the initial inorganic material can be modified by exposing the material to an acid for a certain amount of time and temperature. The chosen acid can have a pH of less than 6, less than 4, or less than 3. Additionally or alternatively, the chosen acid can have a pH in the range of from about 1 to about 6, in the range of from about 2 to about 4, or in the range of from about 4 to about 6. The acid employed during acid pretreatment can be any known or hereafter discovered mineral acid, organic acid, or mixtures of two or more thereof. Furthermore, in various embodiments, the acid employed can also be a chelating agent. Additionally, one or more complexing agents (such as fluoride) can be employed during the acid treatment. In various embodiments, the acid selected for use herein can be a dealuminating acid. Specific examples of acids suitable for use in the various embodiments described herein include, but are not limited to, hydrochloric acid, sulfuric acid, nitric acid, acetic acid, sulfonic acid, oxalic acid, citric acid, ethylenediaminetetraacetic acid (“EDTA”), tartaric acid, malic acid, glutaric acid, succinic acid, and mixtures of two or more thereof. The acid can be in the form of a liquid or a vapor.

During the acid pretreatment, the acid can be present in an amount in the range of from about 1 to about 10, or in the range of from 1.5 to 4 milliequivalents per gram of initial zeolite (“meq/g”). In further embodiments of the acid framework modification, the acid can be present in an amount of at least about 1.5, 2.0, 2.5, 3.0, 3.5, 4.0, or 4.5 meq/g. Furthermore, the acid pretreatment can be performed at a temperature in the range of from about 20 to about 200° C., or in the range of from room temperature to about 100° C. Moreover, the acid treatment can be performed over a time period ranging from about 1 minute to about 12 hours, in the range of from about 1 minute to about 4 hours, or in the range of from 30 minutes to 2 hours.

In other various embodiments, the initial inorganic material can be subjected to additional pretreatments, in addition to those listed above, in order to extract a portion of the aluminum from the initial inorganic material (i.e., dealumination). Additional methods for aluminum removal that may be used in addition to above include, but are not limited to, SiCl₄ vapor treatment and treatment with (NH₄)₂SiF₆,

In cases where pretreatment for aluminum extraction is practiced, composite shaped articles can be formulated so as to be resistant to degradation by the pretreatment process. This can maintain good physical properties in the shaped article and may prevent excessive aluminum extraction from non-zeolitic constituents. If an excessive amount of aluminum is removed from the non-zeolitic constituents of the shaped article, it can result in increased chemical and processing costs to achieve adequate removal of aluminum from the zeolite constituents. This is in addition to the potential for weakening of the non-zeolitic material as a result of acid attack.

As a result of the potential for increased cost or degradation of the shaped article during either an aluminum extraction step or during the process of mesoporosity creation, the non-zeolitic material of the shaped article selected can be resistant to chemical attack under the chosen processing conditions. For example, when extracting aluminum with either an acid or a chelating acid, the non-zeolitic material can be selected based on its degree of resistance to degradation by acid attack, and also to aluminum removal by acid attack. Similarly, under alkaline conditions, such as may be used for mesoporosity creation (discussed below), there is potential for alkali attack upon the non-zeolitic material in the composite shaped article. Thus, the non-zeolitic material may be selected based on its degree of resistance to alkaline attack. In both cases, the term “resistant” means that the material is not degraded to an unacceptable degree. It is not necessary that “resistant” materials be completely unaffected by the respective chemical conditions.

Examples of materials that are resistant to both acidic and alkaline chemical attack include, but are not limited to, inert stable oxides, such as alpha-aluminum oxide, titanium dioxide, zirconium oxide, mullite, hydrous kaolin clay, and the residue of alkaline extraction of kaolin clay which has been calcined through the characteristic exotherm at about 1780° F. without substantial formation of mullite; inert, stable carbides, such as silicon carbide; and inert stable nitrides, such as silicon nitride. Examples of materials resistant to alkaline chemical attack but not acidic attack include, but are not limited to, substantially insoluble alkaline oxides, such as magnesium oxide and calcium oxide.

Mesopore Formation Process

As mentioned above, the pretreated inorganic material (e.g., calcined, acid-treated, heat-treated, and/or steam-treated inorganic material) can be subjected to a mesopore formation process in order to form at least one mesopore in the pretreated inorganic material. Methods for mesopore incorporation contemplated by various embodiments of the present technology (e.g., introduction of mesoporosity in zeolites) can generally include the following steps:

• • 1. Contacting the pretreated inorganic material with a pH controlling medium, optionally in the presence of a pore forming agent, under various time and temperature conditions.
  • 2. Filtering, washing, and drying the zeolite.
  • 3. Removing and/or recovering the pore forming agent (if present), for example, by calcination (removal) and/or chemical extraction (recovery).

The resulting material can also be chemically modified (e.g., by ion exchange with rare earths); blended with binders, matrix, and additives; and shaped (e.g., into beads, pellets, and FCC catalysts).

As noted above, the initial inorganic material can be treated with a pH controlling agent in a pH controlling medium. In one or more embodiments, the pH controlling agent can comprise an acid or a base. In various embodiments, the pH controlling agent comprises a base. Any base can be employed and in any concentration that produces a desired pH range in the pH controlling medium. In various embodiments, the pH controlling medium can have a pH in the range of from about 8 to about 12, in the range of from 9 to 11, or about 10. In other embodiments, the pH controlling medium can have a pH in the range of from about 10 to about 14, in the range of from 11 to 13, or about 12. Examples of bases suitable for use as the pH controlling agent include, but are not limited to, ammonium hydroxide, a tetraalkylammonium hydroxide (e.g., tetramethylammonium hydroxide), and sodium hydroxide. In another embodiment, the base can be selected from the group consisting of ammonium hydroxide, tetraalkyl ammonium hydroxides, sodium hydroxide, potassium hydroxide, sodium carbonate, potassium carbonate, amines, and mixtures of two or more thereof. In certain embodiments, the base comprises a mixture of ammonium hydroxide and sodium hydroxide. In yet another embodiment, the pH controlling medium can further comprise water, such that the pH controlling agent is employed as an aqueous solution.

In other embodiments, the pH controlling agent comprises an acid. Any acid can be employed and in any concentration that produces a desired pH range in the pH controlling medium. In various embodiments the pH controlling medium can have a pH in the range of from about 2 to about 6, in the range of from 3 to 5, or about 4. In other embodiments, the pH controlling medium can have a pH in the range of from about −2 to about 2, in the range of from −1 to 1, or about 0. Examples of acids suitable for use as the pH controlling agent include, but are not limited to, hydrofluoric acid and hydrochloric acid. It should be noted that acids may be of particular use when the initial inorganic material selected for use is a very stable zeolite, such as, for example, ZSM-5, mordenite, or CHA, as discussed above. In various embodiments, the initial inorganic material can first be treated in a pH controlling medium having a low pH for an initial time period. Thereafter, the pH of the pH controlling medium can be increased by adding a base, such as those described above, to increase the pH, such as to the ranges described above.

As noted above, a pore forming agent may optionally be employed along with the pH controlling medium. In one or more embodiments, the pore forming agent can include a surfactant. The order of addition of the surfactant is not critical. In various embodiments, the surfactant can be present in the pH controlling medium prior to introducing the initial inorganic material. In other embodiments, the surfactant can be added to the pH controlling medium following addition of the initial inorganic material. In still other embodiments, a first portion of a first surfactant can be present at the time when the initial inorganic material is introduced and, thereafter, a second portion and/or a second surfactant can be added to the medium.

Surfactants suitable for use can be cationic, anionic, or neutral. In various embodiments, the surfactant comprises a cationic surfactant. In other embodiments, the surfactant comprises an anionic surfactant, a neutral surfactant, or a combination of these. Though not wishing to be bound by theory, it is believed that selection of the surfactant may affect the character of the mesopores introduced into the inorganic material. For instance, surfactants with larger substituents (such as longer pendant alkyl chains) may produce larger mesopores in the inorganic material. Specific examples of surfactants suitable for use include, but are not limited to, alkylammonium halides (e.g., cetyltrimethylammonium bromide (“CTAB”) and cetyltrimethylammonium chloride (“CTAC”)) and PLURONIC® (available from BASF, Florham Park, N.J.). In certain embodiments, when the pH controlling medium has a basic pH (e.g., from about 8 to about 14, or from 9 to 12), the surfactant employed can comprise a cationic surfactant, such as CTAB. In other embodiments, when the pH controlling medium has an acidic pH (e.g., from about −2 to about 6, about −2 to about 2, or about 0), the surfactant employed can comprise an anionic surfactant and/or a neutral surfactant, such as PLURONIC®.

The quantity of surfactant employed can be varied according to the type of surfactant employed and the type of initial inorganic material employed. In various embodiments, the surfactant can be present in a weight ratio with the initial inorganic material in the range of from about 0.01:1 to about 10:1, in the range of from about 0.5:1 to about 2:1, or of about 1:1 surfactant-to-inorganic material based on the combined weight of the surfactant and the initial inorganic material. In various embodiments, the weight of surfactant employed can be about half the weight of the initial inorganic material employed.

In addition to a surfactant, the pH controlling medium can optionally comprise one or more additional reagents. For example, a swelling agent, nanoparticles, biomolecules, a mineralizing agent, a co-surfactant, a metal oxide precursor, a silica solubilizing agent, an alumina solubilizing agent, a triblock copolymer, or any combination thereof, can be added to the pH controlling medium before and/or after introduction of the inorganic material. Such reagents can be selected to control a cross-sectional area of each of a plurality of mesopores introduced into the inorganic material. For instance, use of a swelling agent can expand the surfactant micelles, thereby resulting in larger mesopore formation in the inorganic material.

When contacting the initial inorganic material with a pH controlling medium and, optionally, a surfactant, any time and temperature conditions can be employed that permit mesopore introduction in the initial inorganic material (e.g., the composite shaped article). Generally, the time and temperature conditions are related such that a higher temperature requires a shorter period of time to achieve a desired mesoporosity in the inorganic material resulting in a certain mesostructure. Conversely, a lower temperature may require a relatively longer period of time to achieve the same mesoporosity. Additionally, selection of time and temperature conditions can affect the type of mesostructure that is created in the inorganic material. Thus, by adjusting the synthesis conditions (e.g., pH, time, temperature, inorganic material type, surfactant concentration), different mesostructures (e.g., MCM-41, MCM-48, and MCM-50) can be produced. Because time and temperature are related, any suitable combination of time and temperature may be employed when treating the mixture. For example, the temperature can range from a value in the range of from about room temperature to about 60° C. In other embodiments, the temperature can be in the range from about 30 to about 100° C., in the range of from about 60 to about 100° C., in the range of from 70 to 90° C., or about 80° C. In still other embodiments, the temperature employed can be in the range of from about 100 to about 200° C., in the range of from 100 to 150° C., or about 120° C. In yet other embodiments, the temperature can have a value of at least 100° C.

The time period employed for treatment of the inorganic material can be in the range of from about one hour to about two weeks. In other embodiments, the mixture described above can be held at room temperature and stirred for a time value within the range of from about 1 day to about 1 week. Alternatively, the mixture can be treated for a time period in the range of from about 4 hours to about 1 week.

In one or more embodiments, the controlled time and temperature conditions can take place under hydrothermal conditions, such as, for example, in a sealed reactor where autogenous pressure is created within the sealed reactor. During hydrothermal treatment, the mixture can be stirred by, for example, rotating the vessel (i.e., rotating a sealed reactor or an autoclave). Alternatively or in addition, the contents of the vessel can be stirred by employing one or more stirrers inside the vessel to stir the mixture during the hydrothermal treatment. Stirring the mixture can help avoid sedimentation and may improve distribution of the mixture within the vessel.

In various embodiments, when all or a portion of the surfactant is added to the pH controlling medium after the inorganic material has been added, treatment of the inorganic material can be done at different time/temperatures. For example, in various embodiments, an inorganic material can be treated in a pH controlling medium optionally containing a surfactant under a first set of time/temperature conditions. Thereafter, surfactant can be added to the mixture and the inorganic material can be treated under a second set of time/temperature conditions. Any of the time and temperature conditions described above may be used in such a multi-stage treatment process. Additionally, any of the foregoing process steps can be repeated as desired.

In various embodiments, the resulting mesoporous inorganic materials (described more fully below) can maintain much of their crystallinity subsequent to the above-described treatments. For instance, the mesoporous inorganic materials can have a crystalline content that is at least 5, at least 10, at least 15, at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, or at least 99 percent of the crystalline content of the above-described initial inorganic material, as measured by X-ray diffraction (“XRD”). Additionally or alternatively, the mesoporous inorganic material can have a crystalline content of at least 20, at least 25, at least 30, at least 35, at least 40, at least 45, at least 50, at least 55, at least 60, at least 65, at least 70, at least 75, at least 80, at least 85, at least 90, at least 95, or at least 99 weight percent as measured by XRD.

In one or more embodiments, the resulting mesoporous inorganic materials contain higher mesopore volumes relative to the initial inorganic material subsequent to the above-described treatments. For example, the mesoporous inorganic material can have a 20 to 300 Å diameter mesopore volume that is at least 5, 10, 20, 30, 40, 50, 60, 70, 80, 90, 100, 200, 300, 400, or 500 percent greater than the 20 to 300 Å diameter mesopore volume of the initial inorganic material. In another embodiment, the mesoporous inorganic material has a 20 to 300 Å diameter mesopore volume that is at least 0.02, 0.04, 0.05, 0.06, 0.07, 0.08, 0.09, 0.1, 0.2, 0.3, 0.4, or 0.5 cc/g greater than the 20 to 300 Å diameter mesopore volume of the initial inorganic material. In yet another embodiment, the mesoporous inorganic material has a total 20 to 300 Å diameter mesopore volume of at least 0.05, 0.07, 0.1, or 0.2 cc/g. Additionally or alternatively, the mesoporous zeolite material has a total 20 to 300 Å diameter mesopore volume in the range of from 0.05 to 0.4, 0.07 to 0.35, 0.1 to 0.3, 0.1 to 0.4, or 0.1 to 0.5 cc/g.

When the initial inorganic material employed is a composite shaped article as described above, the above-described process can be sufficient to increase the pore volume of at least one 10 Å subset of mesoporosity in the composite shaped article, thereby forming a shaped zeolitic material with enhanced mesoporosity. As used herein, a “subset of mesoporosity” refers to a sub-range of pore sizes within the 20 to 600 Å range. Thus, a “10 Å subset of mesoporosity” could be any 10 Å range of pore sizes between 20 and 600 Å (e.g., 22-32; 40-50; 135-145; or 499-509 Å). All that is required “to increase the pore volume of at least one 10 Å subset of mesoporosity,” as stated above, is for there to exist at least one 10 Å range of pore sizes between 20 and 600 Å that increases in volume, even if the net mesoporosity over the entire 20 to 600 Å range stays the same or decreases. In various embodiments, the increase in pore volume of the A subset can constitute an increase of at least 0.01, at least 0.04, or at least 0.08 cc/g in that 10 Å subset. Additionally, the increase in pore volume of the 10 Å subset can constitute an increase of at least 10, 20, 30, 40, 50, 60, 70, 80, 90, or 100 percent of the pore volume of the 10 Å subset. In one or more embodiments, the selected 10 Å subset can be contained within a broader range of from 20 to 250 Å, from 20 to 80 Å, or from 30 to 70 Å. In various embodiments, the conditions employed during the above-described process can be sufficient to increase the pore volume of at least one 25 Å subset of mesoporosity in the composite shaped article. In still other embodiments, the conditions employed during the above-described process can be sufficient to increase the pore volume of at least one 50 Å subset of mesoporosity in the composite shaped article.

Additionally, when the initial inorganic material is a composite shaped article, the treatment described above can cause the formation of a plurality of intracrystalline mesopores in the zeolite of the composite shaped article. As used herein, the term “intracrystalline” is intended to denote that the additional mesoporosity is located within the zeolite, as opposed to the non-zeolitic material. Additionally, in various embodiments, the treatment described above can cause a net increase in the overall mesoporosity of the composite shaped article. For example, treatment as described above can cause a net increase in the mesoporosity of at least 0.01, at least 0.05, or at least 0.1 cc/g in the zeolite and/or the non-zeolitic material in the composite shaped article. Furthermore, treatment as described above can cause a net increase of at least 10, 20, 30, 40, 50, 60, 70, 80, 90, or 100 percent in the overall mesoporosity of the composite shaped article. The resulting shaped zeolitic material having enhanced mesoporosity can have a total volume of mesopores in the range of from about 0.05 to about 0.9 cc/g, or in the range of from 0.1 to 0.8 cc/g.

In various embodiments, the treatments described above can allow the initial inorganic material to form a plurality of mesopores having a controlled cross sectional area, thereby forming a mesostructure having long-range crystallinity. Suitable mesostructures include, but are not limited to, hexagonal, cubic, lamellar, foam, random, organized, and controlled. For example, an H—Y[MCM-41] is a mesostructure of an acidic form of faujasite (i.e., H—Y) having long-range crystallinity and having a hexagonal mesopore arrangement (i.e., [MCM-41]). Similarly, an H—Y[MCM-48] is a mesostructure of an acidic form of faujasite having long-range crystallinity and having a cubic pore arrangement. Also, an H—Y[MCM-50] is a mesostructure of an acidic form of faujasite having long-range crystallinity and having a lamellar pore arrangement.

As noted above, the resulting mesoporous inorganic material can be in the form of a mesostructure. Furthermore, when the initial inorganic material comprises a zeolite, the mesoporous inorganic material can be a mesostructured zeolite. The hybrid structure of mesostructured zeolites was studied via X-ray diffraction (“XRD”). FIGS. 1d-3 show the XRD patterns of H—Y[MCM-41], H-MOR[MCM-41], and H-ZSM-5[MCM-41], respectively. As used herein, the naming convention for mesostructured zeolites (e.g., H—Y[MCM-41]) first includes the starting zeolite structure (e.g., H—Y) and then, placed adjacent in brackets, is the name of the mesostructure (e.g., [MCM-41]). The mesostructured zeolite H—Y[MCM-41] retains the full crystallinity of the zeolite H—Y, and features hexagonal pores [MCM-41]. The fully crystalline mesostructure surrounds these hexagonal mesopores that have been formed by the invention. Thus, the resulting structure is a fully crystalline H—Y material that features an [MCM-41] type of mesostructure. For convenience, this is designated as H—Y[MCM-41].

FIG. 1 d depicts the X-ray diffraction pattern of the mesostructured zeolite H-Y[MCM-41], and both the ordered mesostructure MCM-41 (revealed by the XRD peaks at low angles) and the zeolitic fully crystalline structure H—Y are present. FIG. 2 depicts the X-ray diffraction pattern of the mesostructured zeolite H-MOR[MCM-41], and both the ordered mesostructure MCM-41 (revealed by the XRD peaks at low angles) and the zeolitic crystalline structure H-MOR are present. FIG. 3 depicts the X-ray diffraction pattern of the mesostructured zeolite H-ZSM-5[MCM-41], and both the ordered mesostructure MCM-41 (revealed by the XRD peaks at low angles) and the zeolitic crystalline structure H-ZSM-5 are present. Referring now to FIGS. 1d-3, very intense peaks, both at low and high 2° Θ values, reveal both the ordered mesostructure and the zeolitic crystallinity of this family of materials. In all three cases, the peaks at low 2° Θ values can be indexed to hexagonal symmetry indicating the presence of MCM-41, whereas the well-defined XRD peaks at high 2° O values correspond, respectively, to the zeolites Y, MOR and ZSM-5. This observation is remarkable since no long-range crystallinity has been previously observed in mesoporous metal oxides and only semicrystallinity (due to the presence of zeolite nanoclusters) has been achieved in thick-wall mesoporous materials prepared using triblock copolymers.

The connectivity of the mesostructured zeolites was studied by Fourier transform infrared spectroscopy (“FTIR”), the results of which are shown in FIGS. 4 and 5. FIG. 4 depicts FTIR characterization peaks for the fully crystalline mesostructured zeolite H—Y[MCM-41] and zeolite H—Y. The FTIR spectra of the fully crystalline mesostructured zeolite H—Y[MCM-41], labeled Meso-H—Y, is on the top, and the FTIR spectra of the unmodified conventional fully crystalline zeolite H—Y is on the bottom. FIG. 5 depicts FTIR spectra of H—Y[MCM-41] (upper top), H-MOR[MCM-41] (upper middle), H-ZSM-5[MCM-41] (upper bottom), and FTIR spectra of their fully crystalline zeolitic versions in conventional, unmodified form, H—Y (lower top), H-MOR (lower middle), and H-ZSM-5 (lower bottom). The spectra of the fully crystalline mesostructured zeolite H—Y[MCM-41] is the upper top spectra and the spectra of the unmodified fully crystalline zeolite H—Y is the lower top spectra. The spectra of the fully crystalline mesostructured zeolite H-MOR[MCM-41] is the upper middle spectra and the spectra of the unmodified fully crystalline zeolite H-MOR is the lower middle spectra. The spectra of the fully crystalline mesostructured zeolite H-ZSM-5[MCM-41] is the upper bottom spectra and the spectra of the unmodified fully crystalline zeolite H-ZSM-5 is the lower bottom spectra. In FIG. 5 a match between each fully crystalline mesostructured zeolite and its corresponding unmodified fully crystalline zeolite is observed, indicating the zeolitic connectivity is present in fully crystalline mesostructured zeolites. FIG. 5 shows a remarkable match between the IR spectra of the fully crystalline mesostructured zeolites H—Y[MCM-41], H-MOR[MCM-41], and H-ZSM-5[MCM-41] and those of the their corresponding unmodified fully crystalline zeolitic versions, H—Y, H-MOR, and H-ZSM-5, contrary to highly stable Al-MCM-41, which presents only one IR broad peak, due to imperfect zeolitic connectivity. The peak at 960 cm⁻¹ in the H-Y[MCM-41] mesostructured zeolite sample, characteristic of silanol groups on the wall surfaces, provides additional evidence of the mesoporous/zeolitic hybrid nature of mesostructured zeolites.

The presence of well-defined mesoporosity in mesostructured zeolites can be suitably studied by nitrogen physisorption at 77 K. FIGS. 6-8 show the nitrogen isotherms at 77 K of fully crystalline mesostructured zeolites H—Y[MCM-41], H-MOR[MCM-41], and H-ZSM-5 [MCM-41], respectively, and their unmodified zeolitic versions, H—Y, H-MOR, and H-ZSM-5. The presence of well developed narrow pore size diameter distribution mesoporosity is evident in each mesostructured sample. The pore size of the mesoporosity is controlled such that a diameter and/or a cross sectional area of each of the mesopores in a specific fully crystalline mesostructured zeolite falls within a narrow pore size diameter distribution. In one or more embodiments, more than 95% of the mesopores have a pore size (e.g., a diameter and/or a cross sectional area) that falls within plus or minus 75%, 30%, or 10% of the average pore size. Each pore wall or mesopore surface that surrounds a diameter controlled mesopore can be substantially similar in size. Furthermore, the fully crystalline mesostructured zeolites can have a controlled mesoporosity pore size cross sectional area. Where the mesopores are substantially cylindrical in shape, in addition to having a pore size cross sectional area, these pores also have a pore size diameter. However, where the shape of the mesopores are not cylinder-like and are, for example, slit shaped, worm-like (e.g., with a changing diameter throughout at least a portion of the depth of the mesopore surface that surrounds an exemplary mesopore), or non-defined shapes, then at least a portion of such a mesopore surface can have a controlled mesopore cross sectional area. The size of the mesopores is controlled by, for example, the selected surfactant and/or quantity of surfactant used when making a fully crystalline mesostructured zeolite from a conventional unmodified fully crystalline zeolite. Prior attempts to incorporate mesostructures into zeolites have been unable to achieve such a controlled mesoporosity that results in substantially all mesopores in a zeolite having a substantially similar size (e.g., diameter and/or Cross sectional area) and a controlled pore arrangement (e.g., [MCM-41] having a hexagonal pore arrangement). Rather, prior attempts to form mesostructures in zeolites have resulted in any or a combination of a broader pore size distribution ranging from small, medium, to large size pores, different shaped pores, and uncontrolled arrangements.

In various embodiments, a significant volume of mesoporosity can be introduced into the initial inorganic material. For example, referring to FIG. 6, the mesopore volume roughly doubles when the zeolite is mesostructured. In accordance with principles of the invention, in the sample of FIG. 6, the unmodified zeolite H—Y had a mesopore volume of 0.30 cc/g whereas the fully crystalline mesostructured zeolite labeled Meso-HY, which was H-Y[MCM-41], had a mesopore volume of 0.65 cc/g. Conventional zeolites adsorb nitrogen only at low pressures, producing type I isotherms that are characteristic of microporous materials. However, fully crystalline mesostructured zeolites show sharp nitrogen uptakes at higher partial pressures (e.g., P/P₀˜0.3), which is a characteristic feature of mesostructured materials with narrow pore-size distribution (pore diameter ˜2.5 nm). FIGS. 6-8 show similar results for fully crystalline mesostructured zeolites H—Y[MCM-41], H-MOR[MCM-41], and H-ZSM-5[MCM-41], and their unmodified conventional zeolitic versions H—Y, H-MOR, and H-ZSM-5.

FIG. 9 depicts mesostructured zeolite pore volumes (darker columns) of H-Y[MCM-41] (left), H-MOR[MCM-41] (center), and H-ZSM-5[MCM-41] (right) and their zeolitic versions (lighter columns) of H—Y (left), H-MOR (center), and H-ZSM-5 (right). As seen in FIG. 9, compared to conventional zeolites, the fully crystalline mesostructured zeolites have more than double the pore volume due to the incorporation of a well-developed, narrow distribution of pore-size diameter mesoporosity. Referring still to FIG. 9, the volume of mesoporosity that is incorporated can be controlled. The fully crystalline mesostructured zeolite mesoporosity volume can be controlled by, for example, the quantity of surfactant added as a percentage of the quantity of zeolite. Other factors that contribute to mesoporosity volume include the pH, time, and temperature conditions employed. The pore volume is expressed in cubic centimeters of pores over the grams of the zeolite (“cc/g”). The fully crystalline mesostructured zeolite pore volume can be in the range of from about 0.05 cc/g to about 2 cc/g, or from about 0.5 cc/g to about 1 cc/g. The mesopore size is controlled and the mesopore volume can be controlled, for example, by the type and the quantity of surfactant used to create the zeolite mesostructure from the zeolite. The time and temperature conditions may also contribute to the mesopore size and/or the mesopore volume.

In various embodiments, the mesoporous inorganic material prepared as described above can retain substantially the same exterior surface contour (e.g., has substantially the same external size and external shape) and cover substantially the same perimeter as the unmodified initial inorganic material. When the initial inorganic material is a zeolite, suitable unmodified conventional zeolites may range in size from about 400 nm to about 5 microns. In one or more embodiments, the conditions employed to form the mesopores can be selected so as to not substantially change the external size, external shape, or the perimeter of the unmodified zeolite. When a zeolite is employed as the initial inorganic material, the density of the resulting fully crystalline mesostructured zeolite can be less than the density of the unmodified zeolite; the density difference may be due to the zeolite removed when the mesopores were formed. In addition, where the fully crystalline mesostructured zeolite is produced from a fully crystalline conventional unmodified zeolite, the fully crystalline mesostructured zeolite can maintain the full crystallinity of the unmodified conventional zeolite.

Where the unmodified conventional zeolite has a chemical composition in its framework, after mesopores are formed in the conventional zeolite, the chemical composition in the resulting fully crystalline mesostructured zeolite framework can remain substantially the same as the chemical composition in the unmodified conventional zeolite framework that was used as source material. The chemical composition of the unmodified conventional zeolite can vary from the external surface (e.g., about the zeolite perimeter) to the inner core. However, the chemical composition of the unmodified conventional zeolite framework, whether consistent or variable from the perimeter to the inner core of the zeolite, can be unchanged when the mesopores are formed in the zeolite. Thus, in various embodiments, foaming mesopores to create the fully crystalline mesostructured zeolite does not chemically alter the framework of the conventional zeolite. The zeolite stoichiometry can also be unchanged from the unmodified conventional fully crystalline zeolite to the fully crystalline mesostructured zeolite.

Previous attempts by others to form mesostructures in zeolites have resulted in a change in the chemical composition of the framework of the unmodified conventional zeolite. For example, in zeolites containing Si and Al, prior methods treat the zeolite with a base selected to remove more Al than Si from the zeolite. Where such dealumination methods are employed, at least a portion of the chemical composition in the framework of the zeolite changes, specifically, the tetracoordinated alumina ratio changes. In various embodiments described herein, when employing an initial zeolite containing Si and Al, the alumina within the resulting mesostructured zeolite framework can remain tetracoordinated.

Direct evidence for the hybrid single-phase nature of mesostructured zeolites was obtained via transmission electronic microscopy (“TEM”). FIGS. 10a and 10b show two details of the H—Y[MCM-41] mesostructured zeolite microstructure at different foci in which both the crystallinity and ordered mesoporosity can be observed in a single phase. Additional TEM images of mesostructured zeolites are depicted in FIGS. 11 and 12.

Additional evidence of the hybrid nature of mesostructured zeolites comes from catalysis. In various embodiments, the thickness of the pore wall (i.e., the interior wall between adjacent mesopores) can be a value within the range of from about 1 nm to about 50 nm (e.g., ˜2 nm). In addition to other properties, the pore wall thickness makes the mesostructures having long-range crystallinity suitable for catalysis. Their characteristic, in addition to the presence of mesopores and high surface area, appears to allow access to bulkier molecules and reduce intracrystalline diffusion resistance in the long-range crystalline mesostructured zeolites as compared to conventional unmodified long-range crystalline zeolites. Enhanced catalytic activity for bulky molecules is observed in mesostructured zeolites compared to conventional zeolites. For example, semicrystalline mesoporous materials, such as nanocrystalline aluminosilicate PNAs and Al-MSU-S(MFI), show significantly lower activity for cumene cracking (which is usually correlated to strong Bronsted acidity) than conventional H-ZSM-5. Mesostructured zeolites, however, show even greater activity than zeolites, most likely due to their fully zeolitic structure and the presence of mesopores. For example, H-ZSM-5[MCM-41] converts 98% of cumene at 300° C., whereas commercial H-ZSM-5 converts 95% in similar conditions.

Post-Synthesis Treatments of the Mesoporous Materials

As described below in further detail, the mesoporous inorganic material (e.g., the mesostructured material) described above can undergo a variety of post-synthesis treatments. In various embodiments, the mesoporous zeolite can be subjected to one or more post-formation treatments selected from the group consisting of calcination, ion exchange, steaming, incorporation into an adsorbent, incorporation into a catalyst, silicon incorporation, incorporation into a membrane, and combinations of two or more thereof. Suitable ion exchange procedures for the resulting mesoporous zeolite include, but are not limited to, ammonium ion exchange, rare earth ion exchange, lithium ion exchange, potassium ion exchange, calcium ion exchange, and combinations of two or more thereof. Suitable post-formation treatments are described, for example, in U.S. Patent Application Publication No. 2007/0244347, which is incorporated herein by reference in its entirety. Additionally, steps for making the mesostructured material may be repeated or cycled to obtain a desired result. One or more of the hydrothermal treatment conditions, surfactant type, surfactant quantity, and the pH of the pH controlling medium may be altered in each successive cycle.

In one embodiment, a mesoporous inorganic material still present in the synthesis solution may be hydrothermally treated one or more additional times. Specifically, after hydrothermal treatment in the pH controlling media in the optional presence of surfactant and prior to other post-synthesis steps (e.g., filtration, drying, and calcination), one or more of the hydrothermal treatment, surfactant type, surfactant quantity, and pH may be altered in one or more subsequent cycles. Cycles may be employed to further improve the amount, quality, and ordering of the mesoporosity introduced in the inorganic material. Synthesis parameters such as, for example, pH, concentration of surfactant, water content, and mineralization agents, can be adjusted prior to successive hydrothermal treatment. Various cycles of hydrothermal treatment and parameter synthesis can be used. In various embodiments, a fully crystalline mesostructured zeolite can be formed in between about 1 and about 10 cycles, for example. In each cycle, the hydrothermal temperature can vary from about 50 to about 200° C., and the time period allowed for synthesis can vary from about 2 hours to about 2 weeks. Other time and temperatures described above for the initial treatment may also be used.

In various embodiments, after a first hydrothermal treatment, the resulting slurries having an initial pH in the range from about 8 to about 14 can be partially neutralized to a final pH of from about 8 to about 10 by employing acids. Acids suitable for use can be mineral or organic and include, for example, HCl, HNO₃, H₂SO₄, HF, acetic acid, or any combination of such acids. The quantity of surfactant including, for example, quaternary ammonium, phosphonium based surfactants, cationic, neutral, or anionic surfactants, can be increased from about 5 to about 500%. In a second cycle, the same surfactant from the first cycle may be employed. Alternatively, in a second cycle, a second different surfactant or any combination of surfactants may be employed.

In a more particular embodiment, a method for preparing a mesoporous zeolite having a target mesopore volume can comprise:

• • (a) setting a total mesopore volume target for the mesoporous zeolite;
  • (b) treating a first zeolite under first dehydroxylation conditions in a dehydroxylation environment as described above to thereby produce a first dehydroxylated zeolite;
  • (c) treating the first dehydroxylated zeolite under first mesopore forming conditions to thereby produce a first mesoporous zeolite, wherein the first mesopore forming conditions comprise contacting the first dehydroxylated zeolite with at least one pH controlling agent and, optionally, at least one surfactant as described above;
  • (d) measuring the mesopore volume of the first mesoporous zeolite and comparing the mesopore volume of the first mesoporous zeolite to the total mesopore volume target of step (a);
  • (e) treating a second zeolite under second dehydroxylation conditions in the dehydroxylation environment as described above to thereby produce a second dehydroxylated zeolite; and
  • (f) treating the second dehydroxylated zeolite under second mesopore forming conditions to thereby produce a second mesoporous zeolite, wherein the second mesopore forming conditions comprise contacting the second dehydroxylated zeolite with at least one pH controlling agent and, optionally, at least one surfactant as described above.In such an embodiment, the second dehydroxylation conditions and/or the second mesopore forming conditions are adjusted in relation to the first dehydroxylation conditions and/or the first mesopore forming conditions, respectively, according to the results of the comparison of step (d). In one embodiment, the adjustment of the second dehydroxylation conditions of step (e) includes increasing or decreasing the treating time period. In another embodiment, the adjustment of the second dehydroxylation conditions of step (e) includes increasing or decreasing the dehydroxylation temperature. In yet another embodiment, the first and/or second dehydroxylation conditions further comprise contacting the zeolite with steam at a temperature in the range of from about 500 to about 900° C. In such an embodiment, the adjustment of the second dehydroxylation conditions of step (e) includes increasing or decreasing the temperature of the steam and/or the volume of the steam relative to the second zeolite. In still yet another embodiment, the adjustment of the second mesopore forming conditions of step (f) includes increasing or decreasing the amount of the pH controlling agent relative to the zeolite.

In an exemplary synthesis, a zeolite H—Y (Si/Al ˜15) was hydrothermally treated in a sodium hydroxide solution having a pH of 11 and containing the surfactant CTAB at a zeolite-to-CTAB ratio of 1 at 120° C. for 12 hours. After this treatment, 0.2 cc/g of mesoporosity was introduced in the original zeolite, as measured by nitrogen adsorption at 77 K. Pore size distribution was fairly narrow and no mesopore ordering was observed under Transmission Electron Microscopy (“TEM”). In a second cycle, 1.0 M HCl was added until the pH reached 9, an excess of 50% of CTAB surfactant was added to provide a zeolite to CTAB ratio of 1 to 1.5, and second hydrothermal treatment at 120° C. for a 12 hours produced a 0.3 cc/g mesopore volume, a narrower pore size distribution, and same local mesopore ordering, observed by TEM. The materials as modified by changing synthesis parameters and hydrothermal conditions were characterized by X-ray diffraction, gas adsorption, and electronic microscopy. These techniques confirmed that it is possible to control of the synthesis conditions even after some mesoporosity is introduced in the inorganic material. In addition, the successive hydrothermal treatments enable controlled mesoporosity (i.e., controlled pore volume, controlled pore size, and/or controlled pore shape) in the mesostructured material (e.g., a fully crystalline mesostructured zeolite).

Following treatment with the pH controlling agent and the surfactant, the resulting mesoporous inorganic material (which can be a mesostructure having long-range crystallinity) can be separated from the reaction medium. In various embodiments, the step of separating the mesostructured material from the reaction medium can be carried out by one or more methods selected from the group consisting of filtration, centrifugation, and sedimentation. Following separation, the mesoporous inorganic material can be washed and dried. For example, the mesoporous inorganic material can be washed once or repeatedly with water (e.g., deionized water). Additionally, the mesoporous inorganic material can be dried at an elevated temperature. As used herein, the term “elevated temperature” is intended to denote any temperature greater than room temperature. For example, the mesoporous inorganic material can be dried at a temperature in the range of from about 50 to about 100° C.

After separation, washing, and drying, at least a portion of any remaining surfactant, if used, can be removed by, for example, calcination or surfactant extraction. In one or more embodiments, the mesoporous inorganic material can initially be calcined in nitrogen at a maximum temperature from about 500 to 760° C. (or about 1,000 to about 1,400° F.), or at about 550° C.; and then in air for surfactant removal. In various embodiments, the surfactant removal technique can be selected based, for example, on the time needed to remove all or substantially all of the surfactant from the mesoporous inorganic material. In other various embodiments, residual surfactant can be removed via contacting the mesoporous inorganic material with one or more extraction agents under conditions of time and temperature sufficient to extract at least a portion of the residual surfactant. Extraction agents can include, but are not limited to, solvents, acid/solvent mixtures, supercritical fluids, or mixtures thereof. Solvents suitable for use as extracting agents either alone or in combination with an acid include, but are not limited to, an alcohol (e.g., methanol, ethanol, and isopropyl alcohol), acetone, dimethylformamide, methylpyrrolidone, a halogenated solvent, acetonitrile, and mixtures of two or more thereof. Acids suitable for use in an acid/solvent extraction agent include, but are not limited to, inorganic acids, such as hydrochloric acid, nitric acid, or sulphuric acid; organic acids, such as a sulphonic acid, a carboxylic acid, or a halogenated acid; and mixtures of two or more thereof. Supercritical fluids suitable for use as extraction agents include, but are not limited to, carbon dioxide, an alcohol, ammonia, a halogenated methane, a halogenated hydrocarbon, and mixtures of two or more thereof. Whether by calcination and/or extraction agent, in the range of from about 65 to about 100, in the range of from about 75 to about 90, or about 80 weight percent of the surfactant can be removed from the mesoporous inorganic material.

In various embodiments, the mesoporous inorganic material prepared as described above can be modified according to one or more of the following methods, which can be used alone or in combination. For example, at least a portion of the exterior surface (i.e., the geometric surface of the inorganic material) and/or at least a portion of the mesopore surfaces of the mesostructured material (e.g., a fully crystalline mesostructured zeolite) can be modified. Similarly, the surfaces of a crystalline nanostructure, including the external surface of one or more nanostructure members, the surface of one or more pores defined within the members, and/or voids defined between adjacent members, can be modified.

Specifically, the mesostructured material (e.g., a fully crystalline mesostructured zeolite) can accommodate small, medium, and/or large bulky molecules on its surfaces (e.g., the mesoporous surfaces and/or the exterior surface). In various embodiments, the ion exchange properties of the mesostructured materials can be used to introduce chemical species. Much of the surface area that is available and accordingly modified is the surface area of the mesoporous surfaces. The available mesopore surface area in the mesostructured material is controlled, at least in part, by the controlled pore volume. As such, the mesostructured material can be functionalized with a wide variety of chemical groups by various techniques.

In one or more embodiments, various metal alkoxides containing various chemical functionalities can be reacted and grafted to the surface of a mesostructured material (e.g., a fully crystalline mesostructured zeolite) by hydrolysis of the alkoxy groups. In one or more embodiments, a metal trialkoxide (R-M(OR′)₃) can be grafted to the surface of the mesostructured material. For example, trialkoxydes (R-M(OR′)₃) where R is, for example, an amine, a phosphine, a carboxylic acid, an alcohol, or a thiol; where M is Si, Al, Ti, Sn, or Zn; and where R′ is methyl, ethyl, propyl, ethyl, or butyl, are reacted by hydrolysis of the alkoxy group to the surface of the mesostructured material.

These surface-modified mesostructured materials can be prepared by initially degasifying the mesostructured material, which can be in acidic form, under vacuum at a temperature from about 150 to about 550° C. for a time from about 2 to about 24 hours. Alternatively, the sample can be degasified in an inert atmosphere, or it can be air dried at temperatures from about 150 to about 550° C. for a time from about 2 to about 24 hours. The degasified mesostructured material can then be suspended in a dispersing medium. Suitable dispersing mediums can include organic solvents such as, for example, hexane, toluene, xylene, benzene, or any combination of these. Suitable metal alkoxides include, for example, silicon, aluminum, gallium, germanium, zinc, iron, tin, or titanium alkoxides or any combination of these metal alkoxides. The metal alkoxides can include functional groups such as, for example, amines, phosphines, carboxylic acids, hydroxides, thiols, or any combination of these functional groups. A metal alkoxide and/or a functional group can be dissolved in the dispersing medium prior to or after the degasified mesostructured material is suspended in the dispersing medium. The resulting medium can be held at temperatures ranging from about room temperature to about 200° C. Refluxing conditions may also be employed. The sample can be stirred and can be held at the determined temperature for a time period in the range of from about 1 hour to about 1 week. Thereafter, the modified mesostructured material can be filtered, washed (e.g., with the chemical used as a dispersing medium), and dried. The sample can be dried at temperatures ranging from about 20 to about 120° C. and at atmospheric pressure, under inert gas, or under vacuum. The sample can be dried for a time period ranging from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times. In accordance with this treatment, metal alkoxides containing various chemical functionalities can be loaded onto the mesoporous surface and/or the exterior surface of the mesostructured material.

In an exemplary synthesis, 1 gram of fully crystalline mesostructured zeolite H—Y[MCM-41] was degasified under vacuum at 250° C. and was suspended in a 50-mL toluene solution containing 1.5 grams of 3-aminopropyl trimethoxysilane under an argon atmosphere. The suspension was stirred for 12 hours under reflux conditions. Thereafter, the solid was filtered, washed with toluene, and dried at room temperature for 12 hours. Alkylamine grafting was confirmed by infrared spectroscopy.

In other various embodiments, charged chemical species can be introduced to the mesostructured material (e.g., a fully crystalline mesostructured zeolite) by simple ion exchange. Suitable chemical species that can be incorporated by ion exchange include, for example, metal cations, ammonium ions, phosphinium ions, quaternary amines, quaternary phosphines, choline derived compounds, amino acids, metal complexes, or combinations of two or more thereof.

In preparing such materials, a mesostructured material can be suspended in an aqueous solution of a salt of the cation this is to be exchanged by ion exchange. Suitable salts include, for example, sulfates, nitrates, chlorides, or any combination thereof. Suitable cations include, for example, metals, cations of the elements, quaternary ammonium compounds, choline derived compounds, and quaternary phosphonium compounds. The ion and mesostructured material mixture can be stirred for a time ranging from about 1 hour to about 1 week at a temperature ranging from room temperature to about 200° C. Refluxing conditions may also be employed. The sample can then be filtered, washed with water, and dried. The drying temperatures may range from about 20 to about 120° C. at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times. In accordance with this treatment, suitably sized charged chemical species can be loaded onto the mesoporous surface and/or the exterior surface of the mesostructured material. Also in accordance with this treatment, smaller sized charged chemical species can be disposed in the microporous walls.

In an exemplary synthesis, 1 gram of a fully crystalline mesostructured zeolite NH₄—Y[MCM-41] was stirred in 100 mL of a 0.01 M Pt(NH₃)₄(NO₃)₂ aqueous solution for 12 hours at 70° C. The solid was then filtered, washed with deionized water, and dried at 40° C. for 12 hours. This process was repeated three times. Approximately, 1.5 weight percent Pt(NH₃)₄²⁺ was added to the fully crystalline mesostructured zeolite by this ion exchange method.

In other various embodiments, the mesostructured materials (e.g., a fully crystalline mesostructured zeolite) can be neutralized. Specifically, the acidic properties of the mesostructured materials can be used to introduce various chemical species by reaction of the acid sites of the solids with bases containing chemical functionalities of interest. In accordance with this modification of an external surface of the mesostructured material, the mesostructured material can be exposed to a base containing the desired chemical group and the neutralization is simply allowed to happen. These neutralization reactions can be done in a gas, liquid, or solid phase. Also, the external surface of a zeolite can be neutralized by the reaction of the acid sites located on the external surface of the mesostructured zeolite by bulky bases, passivating agents, or poisons.

In preparing such materials, a mesostructured material can be suspended in a dispersing medium in which a certain base is dissolved. Suitable bases include, for example, hydroxides, ammonia, amines, phosphine, or phosphine based bases, or their combinations. The mixture can be stirred for a time period ranging from about 1 hour to about 1 week and can be held at temperatures ranging from room temperature to about 200° C. The sample can then be filtered, washed, and dried. The drying temperature can range from about 20 to about 120° C. at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times. In accordance with this treatment, various chemical species containing chemical functionalities of interest can be loaded onto the mesoporous surfaces and/or the exterior surface of the mesostructured material. Smaller sized chemical species can also be disposed in the microporous walls.

For example, in one exemplary neutralization reaction, 1 gram of a degasified H—Y[MCM-41] fully crystalline mesostructured zeolite was suspended in 20 mL of hexane containing 0.4 mL of triphenylphosphine and stirred for 4 hours in an argon atmosphere. The sample was then filtered, washed with hexane, and dried at room temperature for about 12 hours.

In other various embodiments, various chemical species can be incorporated into and/or with a mesostructured material (e.g., a fully crystalline mesostructured zeolite) using the methods described before, (e.g., ion exchange or neutralization), and can thereafter be reacted to produce a desired solid phase. For example, the fully crystalline mesostructured zeolite NH₄—Y[MCM-41] can be ion exchanged with a Pt(NH₃)₄²⁺ and then heat treated in air at a certain temperature and then in hydrogen at a lower temperature. Heat treatment includes, for example, calcination at temperatures from about 300 to about 600° C. for a time ranging from about 1 hour to about 1 day under dry air and/or nitrogen flow and then under hydrogen flow. The hydrogen concentration can range from 1 to 100% at a temperature from about 200 to about 400° C. for a time period in the range of from about 1 hour to about 1 day. In accordance with this method, when Pt(NH₃)₄—Y[MCM-41] was calcined, Pt(NH₃)₄²⁺ ions reduce to produce highly dispersed Pt nanoparticles on the surface of the mesostructured material.

In other various embodiments, the surface of a mesostructured material (e.g., a fully crystalline mesostructured zeolite) can be coated with various chemical compounds. For example, metal alkoxides (e.g., M(OR′)₄) can be reacted to the surface of the mesostructured material allowing the hydrolysis and the formation of a metal oxide coating on the surface of the mesostructured material. This method includes the passivation of the mesopore surfaces of zeolites. For example, this method enables the formation of a silica coating on the surface of the solid to block the active sites located on the mesopore surfaces of a mesostructured zeolite. In this way, when a zeolite is employed as part of all of the initial inorganic material, the accessibility of the sites in the pore walls can be increased, thereby keeping the shape selectivity typical of conventional zeolites.

In preparing such materials, a mesostructured material (e.g., a fully crystalline mesostructured zeolite), optionally in acidic form, can be degasified under vacuum at temperatures between about 150 and 550° C. for a time between about 2 hours to about 24 hours. Alternatively, the sample can be degasified under an inert atmosphere or air dried at temperatures from about 150 to about 550° C. for a time from about 2 hours to about 24 hours. The degasified mesostructured material can be suspended in an appropriate dispersing medium such as, for example, organic solvents including hexane, toluene, xylene, or benzene, or any combination of these solvents. A metal alkoxide, for example, silicon, aluminum, tin, or titanium alkoxides, can be dissolved in the dispersing medium prior to or after the suspension of the degasified mesostructured material. The mixture can be stirred for a time period ranging from about 1 hour to about 1 week and the mixture can be held at a temperature from room temperature to about 200° C. Refluxing conditions can also be employed. The sample can then be filtered, washed with, for example, the chemical used as a dispersing medium, and dried. The drying temperatures can range from about 20 to about 120° C. at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times.

In other various embodiments, various solid phases, for example, metals, sulfides, oxides, or combinations of these, can be loaded on the surface of the mesostructured material (e.g., a fully crystalline mesostructured zeolite). Various solid phases can be incorporated on the surface of mesostructured material by, for example, impregnation and, if needed, further thermal or chemical treatment. For example, an aqueous nickel acetate solution can be added to a fully crystalline mesostructured zeolite until incipient wetness of the solid. The drying of the solution can be performed slowly, and the resulting solid can be thermally treated. This procedure can yield nickel oxide nanoparticles on the surface of the mesostructured material. Other solid phases that can similarly be loaded by impregnation onto the mesostructured material include sulfide nanoparticles, molybdenum oxide, sulfide, or any other suitable solids known or hereafter discovered in the art.

In preparing such materials, the mesostructured material (e.g., a fully crystalline mesostructured zeolite) can be degasified in vacuum at temperatures from about 150 to about 550° C. for a time period ranging from about 2 hours to about 24 hours. Alternatively, the sample can be degasified under inert atmosphere or dried air at temperatures from about 150 to about 550° C. for a time period in the range of from about 2 hours to about 24 hours. An aqueous solution of the chemical that is to be loaded can be added to the mesostructured material. The contact between the solid and the solution can be maintained for time period from about 1 hour to about 1 week. The contact can be done under vacuum, in an inert atmosphere, or at any air pressure. The final material can be filtered and dried. The drying temperatures can range from about 20 to about 120° C. and be at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled, for example, from 1 time to about 10 times. In accordance with this treatment, various solid phases can be loaded onto the mesoporous surfaces and/or the exterior surface of the mesostructured material.

In an exemplary synthesis, 1 gram of a fully crystalline mesostructured zeolite H—Y[MCM-41] was impregnated (to incipient wetness) with 0.8 mL of a an aqueous solution (0.064 mol 1⁻¹) of ammonium heptamolybdate. Thereafter, the solid was calcined at 500° C. under flowing air. Well dispersed molybdenum oxide nanoparticles were formed inside the micropores, on the surface of the mesopores, and on the exterior surface of the mesostructure.

In other various embodiments, physicochemical properties of mesostructured materials (e.g., fully crystalline mesostructured zeolites) can be controlled by chemical vapor deposition (“CVD”) of various compounds including, for example, metal alkoxides, on to a surface of a mesostructured material. In such embodiments, the mesostructured material can be degassed in vacuum at a temperature ranging from about 200 to about 400° C. It can then be exposed to the chemical compound deposited by CVD. The chemical compound can be, for example, tetramethoxysilane, provided at a certain temperature. This technique can also be used to introduce nanoparticles, carbon, and metal oxide coatings on to the surface of a mesostructured material.

In preparing such materials, the mesostructured material can be degasified in vacuum at temperatures ranging from about 150 and about 550° C. for a time period ranging from about 2 hours to about 24 hours. Alternatively, the sample can be degasified under inert atmosphere or dried air at temperatures ranging from about 150 to about 550° C. for a time ranging from about 2 hours to about 24 hours. Then, the sample can be exposed to the vapors of a chemical compound such as, for example, hydrocarbons, metal complexes, metals, organometallic compounds, or combinations thereof at a temperature and pressure selected to stabilize the vapor phase. This treatment can be conducted for a time period in the range of from about 1 hour to about 1 week. The time period selected depends of the degree of deposition desired. The final material can be washed and dried. The drying temperatures can range from about 20 to about 120° C. at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times. In accordance with this treatment, various chemical compounds can be loaded onto the mesoporous surfaces and/or the exterior surface of the material. Certain small sized vapor molecules may also penetrate the micropores.

In an exemplary synthesis, 1 gram of fully crystalline mesostructured zeolite H-Y[MCM-41] was placed in a quartz reactor and heat treated in a nitrogen atmosphere at 450° C. After 4 hours, the temperature was increased to 700° C. and then a flow of 2.0% propylene in nitrogen was passed at 100 cc/g for 4 hours. This treatment produced a continuous coating of pyrolitic carbon onto the surface of the fully crystalline mesostructured zeolite.

In other various embodiments, a variety of catalysts can be supported on the surface of mesostructured materials (e.g., a fully crystalline mesostructured zeolite). In this way, homogeneous catalysts can be heterogenized. Catalysts can be supported on, for example, the mesopore surfaces and/or on the exterior surface of the mesostructure. Suitable techniques that dispose a catalyst on the mesostructured material include direct ion exchange and chemical species used as ligands to functionalize a surface of the mesostructured material.

In other various embodiments, cationic homogeneous catalysts can be direct ion exchanged with mesostructured materials (e.g., a fully crystalline mesostructured zeolites). Cationic homogeneous catalysts can be used to heterogenize bulky metal complexes to the surface of mesostructured materials. In accordance with this method, cationic species having properties including, for example, optical properties, magnetic properties, electronic properties, bioactivity, or combinations thereof can be heterogenized or immobilized on a surface of the mesostructured material.

Chemical species that contain both a cationic end and a terminal end functional group can be ion exchanged with mesostructured materials. These terminal groups can be used as ligands for heterogenization. Accordingly, the cationic end can be direct ion exchanged with the mesostructured material and the terminal end functional group can modify the chemistry of the surface of the mesostructured material.

In preparing such materials, a mesostructured material can be suspended in an aqueous solution of a salt of the cation that will be ion exchanged. Salts include, for example, sulfates, nitrates, chlorides, or any combinations thereof. Suitable cations include, for example, metals, cations of the elements, quaternary ammonium compounds, choline-derived compounds, and quaternary phosphonium compounds. Any other suitable salts and/or cations known or hereafter discovered may also be employed. The mixture can be stirred for a time ranging from about 1 hour to about 1 week and can be held at temperatures from room temperature to about 200° C. Refluxing conditions may also be employed. Thereafter, the sample can be filtered, washed with water, and dried. The drying temperatures can range from about 20 to about 120° C. at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times. In accordance with this treatment, desirable properties and/or functional groups can be heterogenized to the mesopore surfaces and/or the exterior surface of the mesostructured material.

In an exemplary synthesis, 1 gram of fully crystalline mesostructured zeolite NH₄Y[MCM-41] was stirred in 50 mL of a 0.1 M 5,10,15,20-tetrakis (N-methyl-4-pyridyl) porphyrin pentachloride solution at room temperature for 12 hours. The solid was filtered and washed with deionized water. This process was repeated three times. Finally, the solid was dried under vacuum at 40° C. for 12 hours. As a result of this treatment method, tetrakis (N-methyl-4-pyridyl)porphyrin pentachloride was present on the surface of the fully crystalline mesostructured zeolite.

In another exemplary synthesis, 1 gram of NH₄Y[MCM-41] was stirred in 50 mL of a 0.1 M choline p-toluenesulfonate salt solution at room temperature for 12 hours. The solid was filtered and washed with deionized water. This process was repeated three times. Finally, the solid was dried under vacuum at 40° C. for 12 hours. As a result of this treatment method, choline p-toluenesulfonate was present on the surface of the fully crystalline mesostructured zeolite.

In other various embodiments, the surface of a mesostructured material (e.g., a fully crystalline mesostructured zeolite) can first be functionalized with a chemical species that acts as a ligand and can subsequently be reacted with a metal complex containing ligands. Various chemical species that can act as ligands can be incorporated on the surface of mesostructured material. Methods for incorporating suitable chemical species that act as ligands on the surface of the mesostructured material include, for example, reaction of the mesostructured material with metal alkoxides, ion exchange, neutralization, and other methods selected according to the specific heterogenation application (i.e., the desired chemical species to act as a ligand on the surface of the mesostructured material). In order to heterogenize homogeneous catalysts, chemical species with select properties can be incorporated with ligands to form a metal complex. Suitable chemical species that may be employed as ligands in the metal complex include, for example, amines, phosphines, or combinations thereof.

Following functionalization of the mesostructured material, a metal complex containing ligands can be exposed and allowed to bind to ligands incorporated on the surface of the fully crystalline mesostructured zeolite. Catalyst heterogenization occurs when at least one of the ligands in the metal complex is substituted by at least one ligand attached to the surface of the mesostructured material. Alternatively, catalyst heterogenization occurs when at least one ligand attached to the surface of the mesostructured material is substituted by at least one of the ligands in the metal complex.

In preparing such materials, a mesostructured material containing a chemical group that can be used as a ligand can be degasified under vacuum at a temperature ranging from about 150 to about 550° C. Degasification can take place over a time ranging from about 2 to about 24 hours. Alternatively, the sample can be degasified under inert atmosphere or air dried at temperatures ranging from about 150 to about 550° C. and for a time ranging from about 2 to about 24 hours. The removal of the chemical group (i.e., the ligand) should be avoided; accordingly, the degasification temperatures can range from about 60 to about 200° C. The degasified mesostructured material can be suspended in an appropriate dispersing medium such as, for example, organic solvents including hexane, toluene, xylene, benzene, or any combination thereof. Homogeneous catalysts, for example, metal complexes, enzymes, supramolecular species, organic compounds, or combinations thereof, can be dissolved in the dispersing medium prior to or after suspending the degasified mesostructured material. The resulting mixture can be stirred for a time ranging from about 1 hour to about 1 week at a temperature ranging from room temperature to about 200° C. Refluxing conditions may also be employed. The sample can then be filtered, washed with, for example, the chemical used as dispersing medium, and dried. The drying temperatures can range from about 20 to about 120° C. and be at, for example, atmospheric pressure, under inert gas, or under vacuum. The drying time can range from about 1 hour to about 1 week. This treatment can be repeated or cycled from, for example, 1 time to about 10 times. In accordance with this treatment, catalysts, for example, homogeneous catalysts, can be attached to the mesostructure surface.

In an exemplary synthesis, 1 gram of 3-aminopropyl functionalized fully crystalline mesostructured zeolite H—Y[MCM-41] was reacted in 150 mL of anhydrous ethanol containing 0.1 mol of a metal complex Rh(CO)Cl(L)₂ (where L is a phosphine based ligand) at room temperature for 24 hours under inert atmosphere. After this time, the solid was filtered, washed with anhydrous ethanol and dried at 40° C. under vacuum. The metal complex Rh(CO)Cl was on the surface of the fully crystalline mesostructured zeolite.

In other various embodiments, the chemical composition framework (i.e., the stoichiometry) of a mesostructured material (e.g., a fully crystalline mesostructured zeolite) can be altered. Specifically, metals atoms within the mesostructured material framework can be removed and/or substituted with other elements. Various techniques can be used to substitute some of the metal atoms of the mesostructured material framework with other elements. For example, Al³⁺ can be replaced by Si⁴⁺ by reaction with SiCl₄ in gas phase at high temperature. Other methods to dealuminate mesostructured materials include chemical reaction with EDTA and (NH₄)₂SiF₆, typically under refluxing conditions and at high steam temperatures.

In preparing such materials, the mesostructured material can be exposed to a medium (solid, liquid, or gas) that partially dissolves the mesostructured material. Suitable mediums include, for example, steam, HF, HCl, NaOH, HNO₃, F₂, EDTA, citric acid, or oxalic acid at different concentrations, or any combination thereof. When the mesostructured material is an aluminosilicate (e.g., a zeolite), the medium can remove one or more of the components of the mesostructured material, such as, for example, silica and/or alumina, thereby enriching the mesostructured material framework in the component that was not removed. This treatment can result in a loss in crystallinity in the mesostructured material.

In an exemplary synthesis, 1 gram of H—Y[MCM-41] (Si/Al ˜5) was stirred in 20 mL of a 0.25 M oxalic acid solution at room temperature for 12 hours. The solid was filtered, washed with deionized water, and dried at 60° C. for 12 hours. This treatment resulted in dealumination and crystallinity loss in the mesostructured zeolite.

In various embodiments, the mesoporous inorganic material described above (e.g., a fully crystalline mesostructured zeolite) can be combined with one or more binders and shaped as desired. Suitable binders, such as aluminum oxide, silicon oxide, amorphous aluminosilicates, clays, titania, zirconia, and others can be blended with the mesostructured material, molded, extruded, and heat treated to fabricate pellets, beads, powders (e.g., spray dried substances), layers, a monolith, or any other shapes for use in chemical processing. Binders can similarly be blended with crystalline nanostructures and processed to fabricate shapes for use in chemical processing.

Other phases may be also added to the mesoporous inorganic material for other purposes, such as increasing sulfur tolerance, increasing metal tolerance, increasing catalytic activity, increasing lifetime, increasing selectivity, increasing bottoms upgrading, increasing hydrothermal stability, or any combination thereof. Types of materials employed as other phases include, for example, alumina, silica, calcium oxide, magnesium oxide, antimony passivators, nanosized zeolites, and ZSM-5 zeolite. Suitable methods and techniques for adding phases to the mesostructured materials and to the crystalline nanostructured zeolites are described herein.

In preparing such materials, a mesostructured material, a surface-modified version of a mesostructured material, a crystalline nanostructure zeolite, or a surface-modified version of a crystalline nanostructure zeolite, can be mixed with one or more binders (such as, but not limited to, clays, alumina, silica, or cellulose). These materials can be mixed with the binders in any ratio and with an appropriate amount of water to form a paste that can be mixed. The mixture can be shaped by various methods such as, for example, extruding, molding, spray drying, and pelletizing. Once the solid is shaped, it can be aged by, for example, being treated in air at a temperature ranging from, for example, about 20 to about 200° C. The solid can be treated for a time ranging from about 1 hour to about 1 week. Optionally, in order to increase the solids mechanical properties, it can be heat treated a second time at a higher temperature. The second temperature can vary from about 200 to about 800° C. and for a time period from about 1 hour to about 1 week.

In an exemplary synthesis, 8 grams of a fully crystalline mesostructured zeolite H—Y[MCM-41] was physically mixed with 1.5 grams of bentonite, 0.3 grams of kaolin, and 0.2 g of hydroxyethyl cellulose (dry mixing). Four grams of water was added to the mixture. The resulting medium was additionally mixed. The paste was then extruded, aged, dried, sieved, and calcined at 450° C. for 12 hours.

Exemplary Syntheses of Fully Crystalline Mesostructured Zeolites

As discussed above, FIG. 1a is a schematic illustration of a prior art amorphous mesoporous material 100. As shown in FIG. 1a, zeolite nucleii 105a, 105b, 105c were aggregated around surfactant micelles under controlled conditions to form a solid. Thereafter, the aggregated nuclei 105a, 105b, 105c were washed in water and dried, and the surfactant was extracted to provide a desired mesopore-sized pore volume 110. Each of the zeolite nuclei, for example, 105a, 105b, 105c, is a nanosized crystal. When they are aggregated, the material 100 is polycrystalline because the nuclei material lacks the long-range regular lattice structure of the crystalline state (i.e., the aggregated nuclei are not fully crystalline or truly crystalline). In contrast with FIG. 1a, FIG. 1b is a schematic illustration of a fully crystalline mesostructured zeolite 200, which features a fully crystalline zeolite structure 205 with mesopores 210 penetrating throughout the volume of the zeolite structure 205. The mesostructure 215 that surrounds the mesopores 210 is fully crystalline. The pore wall or interior wall between adjacent mesopores has a wall thickness 230. As illustrated in FIG. 1b, the mesostructure 215 and the mesopores 210 are viewed from a side 220 of the zeolite structure 205. Although not depicted in this schematic illustration, the mesostructure and the mesopores can be viewed from other sides of the mesostructured zeolite 200.

Referring still to FIGS. 1a and 1b, unlike the fully crystalline mesostructure 215 of the fully crystalline mesostructured zeolite 200 depicted in FIG. 1b, in the aggregated crystalline mesoporous zeolite nuclei material 100, the pore walls that surround the mesopore-sized pore volume 110 are discontinuous, featuring multiple zeolite nuclei crystals (e.g., 105a, 105b, 105c).

As discussed above, the synthesis of fully crystalline mesostructured zeolites is applicable to a wide variety of materials. One embodiment is based on the short-range reorganization of a zeolite structure in the presence of a surfactant to accommodate mesoporosity without loss of zeolitic full crystallinity. A zeolite is added to a pH controlled solution containing a surfactant. Alternatively, a zeolite is added to a pH controlled solution and thereafter a surfactant is added. The pH controlled solution can be, for example, a basic solution with a pH ranging from about 8 to about 12, or from about 9 to about 11, or, the basic solution pH can be about 10. The strength of the base and the concentration of the basic solution are selected to provide a pH within the desired range. Any suitable base can be employed that falls within the desired pH range.

As described above, suitable surfactants that can be employed include cationic, anionic, neutral surfactants, or combinations thereof. The quantity of surfactant is varied according to, for example, the surfactant and the zeolite that are mixed. For example, in one embodiment, the weight of surfactant is about equal to the weight of zeolite added to the solution. Alternatively, the weight of surfactant can be about half of the weight of zeolite added to the solution.

The resulting mixture can be hydrothermally treated for a period of time that is selected to allow the fully crystalline zeolite to achieve a desired mesostructure. For example, an H—Y[MCM-41] is a fully crystalline acidic form of faujasite having a fully crystalline mesostructure surrounding a hexagonal pore arrangement. Similarly, an H—Y[MCM-48] is a fully crystalline acidic form of faujasite having a fully crystalline mesostructure surrounding a cubic pore arrangement, and an H—Y[MCM-50] is a fully crystalline acidic form of faujasite having a having a fully crystalline mesostructure surrounding a lamellar pore arrangement. Generally, the time and temperature are related such that a higher temperature requires a shorter period of time to achieve a desired mesoporosity and a certain mesostructure as compared to a lower temperature, which would require a relatively longer period of time to achieve the same mesoporosity. Because time and temperature are related, any suitable combination of time and temperature may be employed when hydrothermally treating the mixture. For example, the temperature ranges from about room temperature to about 60° C.; alternatively, the temperature ranges from 100 to about 200° C. Where the temperature is about 60° C. or greater, the controlled temperature conditions can take place under hydrothermal conditions, for example, in a sealed reactor. The time ranges from about one hour to about two weeks.

In two synthesis experiments, the parameters of time, temperature, zeolite type and quantity, and surfactant type and quantity are kept constant; however, the pH in the first synthesis is 9 and the pH in the second synthesis is 11. As a result of the different pH values in the two synthesis experiments, the two fully crystalline zeolite mesostructures differ from one another. Specifically, the fully crystalline zeolite mesostructure synthesized with the 9 pH solution features fewer mesopore surfaces, because fewer mesopores were incorporated into the conventional fully crystalline zeolite, compared to the fully crystalline zeolite mesostructure synthesized with the 11 pH, which has more mesopore surfaces. Through not wishing to be bound by theory, it is believed that the higher base concentration resulted in increased mesoporosity.

In another exemplary synthesis, a zeolite is added to a diluted NH₄OH solution containing cetyltrimethylammonium bromide (“CTAB”) surfactant. The mixture is hydrothermally treated at about 100 to about 200° C., about 120 to about 180° C., about 140 to about 160° C., or about 150° C., for about 20 hours or overnight, during which the zeolite structure undergoes short-range rearrangements to accommodate the MCM-41 type of mesostructure. Higher surfactant concentrations and longer hydrothermal treatments would produce mesostructured zeolites with the MCM-48 type of mesostructure. After washing and drying, the surfactant is removed by, for example, calcination or surfactant extraction. In one embodiment, the resulting material is calcined in N₂ at a maximum temperature from about 500 to 600° C., or at about 550° C., and then in air for surfactant removal. The surfactant removal technique is selected based, for example, on the time needed to remove all of the surfactant from the mesostructured zeolites. This synthetic scheme could be used to produce mesostructured zeolites with various zeolitic structures.

Without being bound to any one theory, it is believed that the controlled pH solution softens the conventional fully crystalline zeolite surface enabling the surfactant to penetrate the zeolite creating the mesostructured zeolite. More specifically, the pH conditions that are employed enable the surfactant to penetrate the structure of the zeolite; however, it is not believed that the pH conditions dissolve the zeolite. As the surfactant penetrates the zeolite thereby forming mesopores, the penetrated portion is exposed to the controlled pH solution and is softened, enabling further penetration by the surfactant. The penetration continues in this fashion throughout the volume of the zeolite. The penetration through the zeolite volume may be in any single direction or in a combination of directions. For example, the penetration may be through the x direction, the y direction, the z direction, or any combination thereof. The penetration direction or rate is not necessarily linear. Penetration may be ordered or, optionally, the penetration and consequently the mesopores may be disordered or random. Optionally, one or more of the mesopores intersect, interconnect, converge, and/or align, which impacts the arrangement of the resulting mesoporous fully crystalline mesostructure. The surfactant enables penetration into the fully crystalline zeolite, creating mesopores. The type of surfactant determines, at least in part, the size of the mesopore including, for example, the size of the mesopore diameter and/or the size of the mesopore cross section. Penetration into the conventional fully crystalline zeolite is not observed where a controlled pH solution, for example, a base having a pH of 10 held at controlled time and temperature conditions, is mixed with a zeolite without a surfactant.

As mentioned above, certain conventional fully crystalline zeolites are very stable (e.g., ZSM-5, MOR, CHA etc.), and it is difficult to incorporate mesoporosity into these zeolites. In such cases, strong basic solutions having, for example, a pH ranging from about 11 to about 14, or from about 12 to about 13, or an acidic solution, having, for example, a pH ranging from about 2 to about 6, or from about 3 to about 5, or at about 4, may be desired to dissolve silica and soften the conventional fully crystalline zeolite surface to enable the surfactant to penetrate and create mesopores through the fully crystalline zeolite.

Conventional fully crystalline zeolites with a dense structure (e.g. ZSM-5) are more resistant to acids and bases relative to fully crystalline zeolites with less dense structures. Zeolites with a low solubility (e.g., ZSM-5) and/or a dense structure are relatively stable with respect to penetration by acids and bases; accordingly, a diluted tetramethyl ammonium hydroxide (“TMA-OH”) having a pH ranging from about 10 to about 14 or a solution of acid, for example hydrofluoric acid, having a pH ranging from about 2 to about 6 can be used instead of a dilute NH₄OH solution, having a pH ranging from about 9 to about 10, in the synthesis scheme. More specifically, base treatment alone, even at very high pH, might not be sufficient to soften some of the very stable zeolites. The acid HF dissolves silica and softens the structure of the densely structured conventional fully crystalline zeolite (e.g., ZSM-5). After softening the conventional fully crystalline zeolite by exposing it to HF, the pH can be increased by including a base solution having a pH from about 9 to about 11, and a suitable surfactant is added in a quantity selected according to, for example, the quantity of zeolite and the desired mesosporosity volume. The mixture can be treated under appropriate time and temperature conditions to provide the desired mesoporosity and resulting mesostructure in a fully crystalline mesostructured zeolite.

In another exemplary synthesis, a fully crystalline zeolite is added to an acid solution having a pH from about −2 to about 2, or from about −1 to about 1, or about 0, containing a neutral surfactant, for example, PLURONIC® (available from BASF, Florham Park, N.J.). The mixture is exposed to appropriate temperature conditions for a period of time selected to achieve a desired mesostructure. The mixture can be held at room temperature and stirred for from about 1 day to about 1 week. Alternatively, the mixture is hydrothermally treated. In one embodiment, the mixture is hydrothermally treated at about 120° C. for from about 4 hours to about 1 week. The resulting mesopores having a pore diameter measuring from about 5 to 60 nm. A mesopore surface surrounds each mesopore of the mesostructure.

As described above, the mesopore size and architecture may also be conveniently tuned, such as by the use of surfactants with different aliphatic chain lengths, non-ionic surfactants, triblock copolymers, swelling agents, etc. For example, use of a surfactant with a longer chain length increases pore size; conversely, use of a surfactant with a shorter chain length results in smaller pore sizes. Additionally, the use of a swelling agent can expand the surfactant micelles, resulting in larger pore sizes. Any of these mesopore size and mesostructure architecture altering techniques may be used alone or in combination. Also, post-synthesis treatments (e.g., silanation, grafting, surface functionalization, ion-exchange, immobilization of homogeneous catalysts and deposition of metal nanoclusters) can be employed to further improve the textural properties of the materials and/or modify their surface chemistry.

Another aspect features mesostructures such as illustrated in FIG. 1c. Such mesostructures can be achieved based on the dissolution of a zeolite in a pH controlled medium, either in an acidic or basic medium, followed by hydrothermal treatment in the presence of a surfactant. Suitable surfactants that may be employed include cationic, anionic, neutral surfactants, and/or combinations thereof. The quantity of surfactant is varied according to, for example, the selected surfactant and the selected zeolite. For example, the weight of surfactant can be about equal to the weight of zeolite added to the solution; alternatively, the weight of surfactant can be about half of the weight of zeolite and that dissolves the zeolite ranges from about 10 to about 14. Where the pH controlled medium is acidic, the pH ranges from about −2 to about 2; when using HF, the pH range is from about 2 to about 6. Under these more extreme pH conditions, a mesoporous solid can be obtained where the pore walls are initially amorphous. The pore walls can later be transformed to a zeolitic phase, with or without affecting the mesoporous structure. More specifically, after the zeolite is exposed to this aggressive pH treatment, the pH can be adjusted to about 10 by adding, for example, NH₄OH and surfactant (e.g., CTAB) to produce self-assembling partially dissolved zeolites. This synthesis mixture can be hydrothermally treated or stirred at room temperature over a period of time to obtain a highly stable mesoporous amorphous aluminosilicate. More specifically, if the synthesis mixture is hydrothermally treated at, for example, from about 100 to about 150° C., a highly stable mesoporous amorphous aluminosilicate can be obtained. Alternatively, the synthesis mixture can be stirred at room temperature for sufficient time (from about 4 hours to about 1 day) to obtain a highly stable mesoporous amorphous aluminosilicate. The mesoporous amorphous aluminosilicate maintains its mesoporosity after boiling for 48 hours under reflux conditions. The acidity of the material produced is higher than that of amorphous mesoporous materials obtained from non-zeolitic silica and alumina sources. Where the synthesis mixture is hydrothermally treated for a longer period of time (from about 12 hours to about 2 weeks) a zeolitic mesostructure is obtained. By adjusting the synthesis conditions (e.g., pH, time, temperature, zeolite type, surfactant concentration) different zeolite nanostructures (e.g., nanotubes, nanorings, nanorods, nanowires, nanoslabs, nanofibers, nanodiscs, etc.) can be produced. Referring again to FIG. 1c, a nanostructure including, for example, nanorods is made from adjacent members (e.g., a first nanorod adjacent a second nanorod). Voids can be formed between adjacent members (e.g., adjacent nanorods). Each nanostructure member defines a plurality of pores (e.g., each nanorod has pores in its structure). Different members can join together within a single nanostructure, for example, a nanorod may be adjacent a nanoring.

Zeolitic nanorods (“ZNRs”) have been prepared by this approach in three steps: (i) basic treatment of a zeolite in a pH controlled medium to partially dissolve the zeolite and produce a suspension of amorphous aluminosilicate, (ii) pH adjustment and surfactant addition to produce MCM-41, and (iii) hydrothermal treatment of the resulting solid at a temperature typically ranging from about 100 to about 200° C. for from about 12 hours to about 2 weeks. During the last step, the MCM-41 (the hexagonal pore arrangement) mesostructure is first transformed to MCM-48 (the cubic pore arrangement) and is then transfotined to MCM-50 (the lamellar pore arrangement), while the amorphous pore walls are transformed to a crystalline zeolitic phase. MCM-50 is a lamellar structure and is a precursor to zeolitic nanostructures including, for example, nanotubes, nanorings, nanorods, nanowires, nanoslabs, etc. The specific nanostructure formed by using steps (i)-(iii) is determined by the selected zeolite, surfactant, temperature, time, and pH. The zeolite and other conditions can be selected to achieve a single nanostructure shape (e.g., all nanorod) or, alternatively, multiple nanostructure shapes. Without being bound to any single theory, it appears that nanostructures are achieved, at least in part, because the zeolite dissolved by a pH controlled solution into a suspension of amorphous aluminosilicate retains some degree of the zeolitic connectivity that is characteristic of a zeolite starting material. It is expected that some of the IR spectra bands characteristic of zeolites remain present in the dissolved solution (i.e., in the suspension of amorphous aluminosilicate). In contrast, if, rather than dissolving a zeolite to produce a suspension of amorphous aluminosilicate, an alumina, a silica, or an amorphous aluminosilicate were exposed to steps (ii)-(iii), described above, the nanostructure fails to form. The building blocks of connectivity present in dissolved zeolite solution appear to play a part in forming nanostructures.

Although the nanostructures are crystalline they are not fully crystalline. They have a few units in one direction and are semi crystalline or are polycrystalline. Semi crystalline and polycrystalline refer to, for example, nanosized crystals, crystal nuclei, or crystallites that, for example, aggregate to form a solid. Unit cells are the simplest repeating unit in a crystalline structure or crystalline material. Nanostructures have an open structure. They have a high surface area due to an extended structure in the space as well as due to spaces between multiple structures or voids within the structures themselves. Generally, these nanostructures also have a high external surface area. In one embodiment, one nanostructure is adjacent another nanostructure. FIG. 1c depicts a TEM image of a nanostructured zeolite where the nanostructure shape includes nanorods. The nanorods have a thickness measuring about 5 nm. As depicted, the nanorods sit adjacent one another and the nanorods curve. The background of the curved rods seen in the TEM image is noise and it should be ignored.

Applications

The unique structure of mesostructured materials will be useful to a variety of fields, and should address certain limitations associated with conventional zeolites. Examples of such applications include, but are not limited to, hydroisomerization of paraffinic feed stocks; isomerization of C-8 aromatics (e.g., ortho-, meta-, or para-xylene, and ethylbenzene); alkylation of aromatics (e.g., alkylation of benzene with ethylene or propylene); oligomerization of olefins; FCC additives for increased olefin production and octane increase; upgrading of Fischer Tropsch liquid products; upgrading of hydrocarbon liquids produced from biomass feed stock; conversion of olefins to aromatics; dewaxing of paraffinic feeds; disproportionation of alkylaromatics (e.g., toluene disproportionation to xylenes and benzene); and applications in gas separation, a process where rapid adsorption and desorption are required. As catalysis is an important field of application for zeolites, special emphasis is placed on the catalytic applications of mesostructured zeolites.

The combination of a mesostructure, a high surface-area, and controlled pore or interior thickness as measured between adjacent mesopores should provide for access to bulky molecules and reduce the intracrystalline diffusion barriers. Thus, enhanced catalytic activity for bulky molecules should be observed over mesostructured zeolites, as compared to conventional zeolites. See FIGS. 13 and 14. The subject matter of FIGS. 13-20a involves reactions with 1,3,5-triisopropylbenzene being catalytically cracked to form 1,3-diisopropyl benzene. The 1,3,5-triisopropylbenzene is representative of molecules present in crude oil and 1,3-diisopropyl benzene is representative of a product within the gasoline range. These experiments are a surrogate for molecules present in crude oil that are cracked to form gasoline.

FIG. 13 depicts the process of catalytic cracking of 1,3,5-triisopropyl benzene by zeolite H—Y. Catalytic cracking is selectivity and/or efficiency limited, because diffusion is limited by the small pore size of the zeolite H—Y. Because the conventional unconverted zeolite crystal has limited diffusion, it is difficult for the initial reaction product (e.g., 1,3-diisopropyl benzene) to exit the zeolite. As a result, over cracking occurs and light compounds are formed resulting in excess formation of undesirable products, such as cumene, benzene, and coke. FIG. 14 depicts the process of catalytic cracking of 1,3,5-triisopropyl benzene by a mesostructured zeolite. In contrast to catalytic cracking with the unmodified conventional zeolite H—Y, the larger pore size, the controlled mesopore volume, and the controlled interior or pore wall thickness present in the fully crystalline mesostructured zeolite facilitates the exit of desired products (i.e., 1,3-diisopropyl benzene) from the mesostructure, and over cracking that produces cumene, benzene, and coke is avoided. As a result, there is a higher conversion of the desired product, 1,3-diisopropyl benzene.

Acid catalysts with well-defined ultra-large pores are highly desirable for many applications, especially for catalytic cracking of the gas oil fraction of petroleum, whereby slight improvements in catalytic activity or selectivity would translate to significant economic benefits. As a test reaction, we have examined the catalytic cracking of 1,3,5-triisopropylbenzene (critical dimension 0.95 nm) to produce 1,3-diisopropyl benzene. FIG. 15 depicts catalytic activity for 1,3,5-triisopropyl benzene cracking shown as percent conversion to 1,3-diisopropyl benzene vs. time for the mesostructured zeolite H—Y[MCM-41], which is labeled Meso-HY, the zeolite H—Y, and a conventional Al-MCM-41. Catalytic cracking was performed when 50 mL/min of He saturated with 1,3,5-triisopropylbenzene at 120° C. was flowed at 200° C. over 50 mg of each catalyst. The H—Y[MCM-41] mesostructured zeolite demonstrated superior catalytic activity for this cracking reaction after 400 minutes at 200° C. (93% conversion) compared to the H—Y zeolite (71% conversion) and the mesoporous Al-MCM-41 (39% conversion) (see FIG. 15). This result was attributed to its combination of strong acidity and mesostructured nature. The mesopores and the mesostructure surrounding the mesopores greatly facilitated the hydrocarbon diffusion within the H—Y[MCM-41] catalyst thereby improving conversion. The H—Y[MCM-41] mesostructured zeolite is stable and maintains mesostructure integrity even under harsh conditions. FIG. 17 depicts the hydrothermal stability of H—Y[MCM-41], labeled Meso-HY, compared to the non-mesolytic zeolite Al-MCM-41. For example, the boiled mesostructured zeolite H—Y[MCM-41], labeled Meso-HY, also maintained its physicochemical integrity even after being boiled for several days, exhibiting a high 1,3,5-triisopropylbenzene activity (87% conversion to 1,3-diisopropyl benzene after 400 minutes) even after such severe treatment. The term boiled is used for convenience; however, the specific treatment to the material includes suspending the solid in water and heating the water and solid material under reflux conditions. See FIG. 17. This outcome illustrates the superior hydrothermal stability of H—Y[MCM-41] over the amorphous Al-MCM-41 catalyst, which lost its activity and ordered mesostructure after exposure to similar conditions. These results show that hydrothermally stable H—Y[MCM-41] is a crystalline material and its crystallinity contrasts the amorphous Al-MCM-41 catalyst that structurally collapsed after boiling, rendering it unable to convert appreciable quantities via catalytic cracking.

FIG. 19 depicts catalytic activity for 1,3,5-triisopropyl benzene cracking shown as percent conversion vs. time for H-ZSM-5[MCM-41], labeled Meso-H-ZSM-5, and its zeolitic version, H-ZSM-5. A 50 mL/min He flow saturated with 1,3,5-triisopropylbenzene at 120° C. was flowed at 200° C. over 50 mg of each catalyst, H-ZSM-5[MCM-41] and H-ZSM-5. H-ZSM-5 is used as an important additive in cracking catalysts to increase propylene production and improve octane number in gasoline. However, due to its small pores, H-ZSM-5 is inactive in 1,3,5-triisopropylbenzene cracking at 200° C. (<1% conversion to 1,3-diisopropyl benzene after 400 min). The incorporation of MCM-41 mesostructure in this zeolite (H-ZSM-5[MCM-41]) successfully achieved substantial activity, with 40% conversion of 1,3,5-triisopropylbenzene to 1,3-diisopropyl benzene after 400 min (see FIG. 19). In this case, the activity was attributed to the mesopores and strong acidity of the mesostructured zeolite.

More than 135 different zeolitic structures have been reported to date, but only about a dozen of them have commercial applications, mostly the zeolites with 3-D (3-dimensional) pore structures. The incorporation of 3-D mesopores may be beneficial for zeolites with 1-D and 2-D pore structures as it would greatly facilitate intracrystalline diffusion. Zeolites with 1-D and 2-D pore structures are not widely used, because the pore structure is less then optimal. To illustrate the potential of mesostructure processing of zeolites with low pore interconnectivity, H-MOR with 1-D pores were prepared with an MCM-48 mesostructure by exposing the H-MOR zeolite with 1-D pores to a pH controlled solution in the presence of a surfactant under suitable time and temperature conditions, described above. The resulting H-MOR[MCM-48] with 3-D mesostructured structures was examined for the catalytic cracking of 1,3,5-triisopropylbenzene at 200° C. FIG. 18 depicts catalytic activity for 1,3,5-triisopropyl benzene cracking shown as conversion to 1,3-diisopropyl benzene vs. time for H-MOR[MCM-48] labeled Meso-HMOR, and its zeolitic version, H-MOR. A 50 mL/min He flow saturated with 1,3,5-triisopropylbenzene at 120° C. was flowed at 200° C. over 50 mg of each catalyst, H-MOR[MCM-48] and H-MOR. Catalytic cracking with H-MOR[MCM-48] exhibited 50% conversion after 400 minutes, which was significantly higher compared to the 7% conversion achieved by H-MOR (see FIG. 18). Zeolites with 1-D pore structures show a more dramatic improvement when exposed to the mesostructure process as compared to the zeolites with 2-D pore structures, but this is to be expected because the 1-D pore structure zeolites begin with provide more limited diffusion. When exposed to the mesostructure process, zeolites with 2-D pore structures result in 3-D mesostructures. Exposing 1-D and 2-D pore structure zeolites to the instant process for forming mesostructures in fully crystalline inorganic material may increase the usefulness of these otherwise underused zeolites.

Mesostructured zeolites not only showed much higher catalytic activity, but also enhanced selectivity over zeolites. Referring now to FIG. 16, a commercially available zeolite H—Y was employed to catalytically crack 1,3,5-triisopropylbenzene. The resulting products were 1,3-diisopropyl benzene, benzene, and cumene and the fractional composition results were normalized to be 100%. The mesostructured zeolite, labeled Meso-HY, which is H—Y[MCM-41], was employed to catalytically crack 1,3,5-triisopropylbenzene under identical conditions employed with H—Y. Increased production of 1,3-diisopropyl benzene (about 110% of the 1,3-diisopropyl benzene produced with the zeolite H—Y) and decreased production of benzene and cumene (about 75% of the benzene and cumene produced with the zeolite H—Y) was observed. In this example, H—Y[MCM-41] mesostructured zeolite produced only 75% of the benzene generated by the H—Y zeolite. See FIG. 16. Benzene is a toxic compound whose presence in gasoline is being increasingly restricted by legislation. The benzene production was even lower in the case of H-MOR[MCM-48], and was minimal in the ease of H-ZSM-5[MCM-41]. The decrease in benzene production has been observed in small zeolite crystals, and was related to the intrinsic ability of crystals with higher surface areas to limit successive cracking reactions. It also reduced the formation of coke, which is an undesired end-product of the cracking process that can be responsible for catalyst deactivation. Thus, the mesostructured zeolites not only provided for higher catalytic activity and selectivity, but also longer catalyst life time.

Zeolitic nanorods another form of mesostructured zeolite, also enhance catalytic activity by increasing active-site accessibility. The rod-shape ZNRs are only nanometer-sized in diameter, so internal diffusional resistance is minimal. These new mesostructured zeolites (also referred to as nanostructures) were tested as cracking catalysts for the gas oil fraction of petroleum to assess their potential. FIG. 20a depicts, on the left-hand side Y axis, the percent conversion of 1,3,5-triisopropylbenzene to 1,3-diisopropyl benzene versus time for H-MOR[ZNR] and H-MOR. The ratio of benzene produced by H-MOR-to-benzene produced by H-MOR[ZNR] as a function of time is also shown on the secondary Y axis located on the right-hand side of FIG. 20a, and an arrow is present on the line that connects this data. A helium flow of 50 mL/min saturated with 1,3,5-triisopropylbenzene at 120° C. was introduced over 50 mg of each catalyst, H-MOR[ZNR] and H-MOR, at 200° C.

In the cracking of 1,3,5-triisopropylbenzene, the conventional H-MOR zeolite showed a low activity (7% conversion to 1,3-diisopropyl benzene after 400 min) due to its medium-sized (0.65 to 0.70 nm), 1-D pores. In contrast, H-MOR[ZNR] achieved a much higher catalytic activity under similar conditions (52% conversion to 1,3-diisopropyl benzene) (see FIG. 20a). This significant increase in catalytic activity was attributed to ZNRs' higher surface areas, readily accessible active sites, and improved intracrystalline diffusivity.

Besides increased activity, ZNRs also showed improved selectivity due to their nanostructured rod-shape morphology. For example, H-MOR[ZNR] produced 3 times less benzene per mole of 1,3,5-triisopropylbenzene converted as compared to the commercial zeolite H-MOR (see the secondary Y axis on the right-hand side of FIG. 20a). Benzene may include, for example, benzene derivatives such as, for example, toluene, xylene, and other related derivative compounds. This significant increase in selectivity also helped to reduce coke formation, which has been a major problem with conventional cracking catalysts, especially those containing 1-D pores, such as mordenite.

The simple, inexpensive, and generalized synthesis strategies described herein allow for the preparation of ZNR, a crystalline material with walls that are only several nanometers thick (e.g., 3-20 mu), in which nanorings and junctions are common. The novel synthesis strategies were based on the “programmed” zeolitic transformation of mesoporous materials, which avoided the typical drawbacks of nanoscaled zeolite synthesis (e.g., low yield, difficulty in separation, and high pressure drops) and did not require the use of a layered precursor. The unique crystalline structure of ZNRs provided for improved catalytic conversion of bulky molecules by increasing the accessibility to its microporosity, while reducing interparticle and intraparticle diffusion barriers.

Referring now to FIGS. 20b and 20c, mesostructured zeolites were tested for crude oil refining via Microactivity Test (“MAT;” ASTM D-3907). This is a well known and widely accepted technique to estimate the performance of fluid catalytic cracking (“FCC”) catalysts. Vacuum gas-oil was used as feed in a fluid-bed stainless steel reactor. The experiments were conducted under identical conditions with mesostructured zeolites and their conventional zeolites counterparts.

FIG. 20 b depicts MAT results of a conventional fully crystalline zeolite H—Y (Si/Al ˜15) and its fully crystalline mesostructured version H—Y[MCM-41]. MAT conditions included a reaction temperature of 500° C., a catalyst contact time of 60 seconds, a catalyst charge of 1 gram, a catalyst/vacuum gas oil ratio of 2, and a WHSV of 30 g/h/g. The conversion (i.e., how much of the vacuum gas oil feed was converted into product), with all yield normalized to 100% for comparison purposes, for the unmodified fully crystalline zeolite H—Y was 61.22%, and for the fully crystalline mesostructured zeolite H—Y[MCM-41] was 67.20%. Although not depicted in FIG. 20b, the results of this test provided liquid petroleum gases (“LPG”) fraction of H—Y of 17.45% and LPG fraction of H—Y[MCM-41] of 15.27%.

FIG. 20 c depicts the composition of the LPG fraction obtained by MAT of a conventional fully crystalline zeolite H—Y (Si/Al ˜15) and its fully crystalline mesostructured version H—Y[MCM-41], described above in conjunction with FIG. 20b. The composition of the LPG fraction was analyzed to determine the components of the LPG fraction. Where the fully crystalline zeolite H—Y was used, the LPG fraction was 17.45%. Where the fully crystalline mesostructured zeolite HY[MCM-41] was used, the LPG fraction was 15.27%. In addition, the fully crystalline mesostructured zeolites produced more olefins, which are desired products. Referring now to the X-axis on FIG. 20c, the label C3 indicates propane, the label C3=indicates propene, the label i-C4 indicates isobutane, the label n-C4 indicates normal butane, the label i-C4=indicates isobutene, and the label n-C4=indicates normal butene. Specifically, the fully crystalline mesostructured zeolite produced increased propene, isobutene, and normal butene in the LPG fraction as compared to the unmodified fully crystalline zeolite. Further, the fully crystalline mesostructured zeolite produced a lesser fraction of LPG than with its counterpart conventional unmodified fully crystalline zeolite. The internal wall thickness of the fully crystalline mesostructured zeolite is less than the internal wall thickness of the unmodified fully crystalline zeolite. Thus the thinner internal walls in the fully crystalline mesostructured zeolites reduced hydrogen transfer reactions, which are responsible for the undesired conversion of olefins to paraffins. Accordingly, an increased number of desired olefins are produced where fully crystalline mesostructured zeolites are used instead of conventional unmodified fully crystalline zeolites.

In the MAT, generally, the samples were displayed in a fluidized-bed stainless steel reactor. Reaction temperature was 500° C., the amount of catalyst was 3.0 g, the catalyst/oil ratio was 2.0, the WHSV was 30 g/h/g, and the contact time was 60 seconds. These tests showed that using H—Y[MCM-41] in place of conventional H—Y resulted in a 43% increase in gasoline production, a 75% increase in propylene and a 110% increase in butenes. Additionally, there is a 32% decrease in coke formation, a 23% decrease in total dry gas, and a 12% decrease in LPG. The presence of mesopores in the H—Y[MCM-41], which has at least double the surface area of H—Y, favors the cracking of the larger molecules present in the crude oil, which cannot be transformed within the micropores of conventional zeolites. Typically, conventional zeolites have pores measuring about 0.7 nm, which are too small to efficiently process desirable products, for example, alkyl benzene, contained in heavy crude oil fractions. Larger pore sizes are required to facilitate improved surface area contact (including within the pore walls or mesopore surfaces) with the hydrocarbon materials. For comparison, the diameter of each of the mesopores, which are surrounded by the mesopore surfaces of the fully crystalline mesostructure of the invention, can measure, e.g., about 2 nm. The increased production of light olefins was related to the reduction of hydrogen transfer reaction due to the presence of favorable interior or pore wall thickness in the fully crystalline mesostructured zeolites (e.g., ˜2 nm) as opposed to the thick crystals of conventional zeolites (e.g., ˜1000 nm). This interior or pore wall thickness also results in reduction of over-cracking, significantly reduces coke formation, and reduces production of total dry gas and LPG.

Pyrolysis of plastics has gained renewed attention due to the possibility of converting these abundant waste products into valuable chemicals while also producing energy. Acidic catalysts, such as zeolites, have been shown to be able to reduce significantly the decomposition temperature of plastics and to control the range of products generated. However, the accessibility of the bulky molecules produced during plastic degradation has been severely limited by the micropores of zeolites.

The catalytic degradation of polyethylene (“PE”) by commercially available zeolites and their corresponding mesostructured zeolites was studied by thermal gravimetric analysis (“TGA”). FIG. 21 depicts the percentage of polyethylene weight lost vs. temperature for the following mixtures of catalysts in weight ratio to PE. The curves labeled (A)-(G) depict results of the following degradation curves: (A): no catalyst, (B): H-ZSM-5:PE, 1:2; (C): H-ZSM-5[MCM-41]:PE, 1:2; (D): H-ZSM-5:PE, 1:1; (E) H-ZSM-5:PE, 2:1; (F): H-ZSM-5[MCM-41]:PE, 1:1; and (G) H-ZSM-5[MCM-41]:PE, 2:1. In all cases, fully crystalline mesostructured zeolites allow for reduced decomposition temperatures compared to unmodified commercial zeolites (by ˜35° C. in the case of (C)H-ZSM-5[MCM-41] vs. (B) H-ZSM-5), even at high catalyst:PE ratios (see FIG. 21). In fact, referring to the curve labeled (F), with an H-ZSM-5[MCM-41]:PE weight ratio of 1:1, a lower decomposition temperature was achieved compared to that required by referring to curve labeled (E), a ZSM-5:PE weight ratio of 2:1.

With their improved accessibility and diffusivity compared to conventional zeolites, fully crystalline mesostructured zeolites may also be employed in place of unmodified conventional zeolites in other applications, such as gas and liquid-phase adsorption, separation, catalysis, catalytic cracking, catalytic hydrocracking, catalytic isomerization, catalytic hydrogenation, catalytic hydroformilation, catalytic alkylation, catalytic acylation, ion-exchange, water treatment, pollution remediation, etc. Many of these applications suffer currently from limitations associated with the small pores of zeolites, especially when bulky molecules are involved. Mesostructured zeolites present attractive benefits over zeolites in such applications.

Organic dye and pollutant removal from water is of major environmental importance, and represents the third major use of zeolites (accounting for 80 tons of zeolites per year). However, most of the organic dyes are bulky, which make their removal slow or incomplete, requiring a huge excess of zeolites in the process. Fully crystalline mesostructured zeolites offer significant advantage over unmodified conventional zeolites in organic dye and pollutant removal with their larger surface area and pore size.

Application in Petrochemical Processing

The mesostructured materials can have one or more of controlled pore volume, controlled pore size (e.g., cross sectional area and/or diameter), and controlled pore shape. Hydrocarbon reactions, including petrochemical processing, are mass-transfer limited. Accordingly, a fully crystalline mesostructured catalyst with controlled pore volume, pore size, and/or pore shape can facilitate transport of the reactants to and within active catalyst sites within the fully crystalline mesostructured catalyst and transport the products of the reaction out of the catalyst. Fully crystalline mesostructured inorganic materials, for example, zeolites, enable processing of very large or bulky molecules, with dimensions of, for example, from about 2 to about 60 nm, from about 5 to about 50 nm, and from about 30 to about 60 nm.

Hydrocarbon and/or petrochemical feed materials that can be processed with the mesostructured materials (e.g., fully crystalline mesostructured zeolitic materials) and/or the crystalline nanostructure materials include, for example, a gas oil (e.g., light, medium, or heavy gas oil) with or without the addition of resids. The feed material can include thermal oils, residual oils, (e.g., atmospheric tower bottoms (“ATB”), heavy gas oil (“HGO”), vacuum gas oil (“VGO”), and vacuum tower bottoms (“VTB”)), cycle stocks, whole top crudes, tar sand oils, shale oils, synthetic fuels (e.g., products of Fischer-Tropsch synthesis), heavy hydrocarbon fractions derived from the destructive hydrogenation of coal, tar, pitches, asphalts, heavy and/or sour and/or metal-laden crude oils, and waxy materials, including, but not limited to, waxes produced by Fischer-Tropsch synthesis of hydrocarbons from synthesis gas. Hydrotreated feedstocks derived from any of the above described feed materials may also be processed by using the fully crystalline mesostructured zeolitic materials and/or the crystalline nanostructure materials.

Heavy hydrocarbon fractions from crude oil contain most of the sulfur in crude oils, mainly in the form of mercaptans, sulfides, disulfides, thiophenes, benzothiophenes, dibenzothiophenes, and benzonaphthothiophenes, many of which are large, bulky molecules. Similarly, heavy hydrocarbon fractions contain most of the nitrogen in crude oils, principally in the form of neutral N-compounds (indole, carbazole), basic N-compounds (pyridine, quinoline, acridine, phenenthridine), and weakly basic N-compounds (hydroxipyridine and hydroxiquinoline) and their substituted H-, alkyl-, phenyl- and naphthyl-substituted derivatives, many of which are large, bulky materials. Sulfur and nitrogen species are removed for production of clean fuels and resids or deeper cut gas oils with high metals content can also be processed using the mesostructured materials and/or the crystalline nanostructure materials described herein.

In various embodiments, the mesostructured material and/or the crystalline nanostructured material can be employed in chemical processing operations including, for example, catalytic cracking, fluidized catalytic cracking, hydrogenation, hydrosulfurization, hydrocracking, hydroisomerization, oligomerization, alkylation, or any of these in combination. Any of these chemical processing operations may be employed to produce, for example, a petrochemical product by reacting a petrochemical feed material with the mesostructured material and/or the crystalline nanostructured materials described herein.

In various embodiments, the mesostructured material and/or the crystalline nanostructured material can be used as an additive to other catalysts and/or other separation materials including, for example, a membrane, an adsorbent, a filter, an ion exchange column, an ion exchange membrane, or an ion exchange filter.

In various embodiments, the mesostructured material and/or the crystalline nanostructured material can be used alone or in combination as an additive to a catalyst. The mesostructured material and/or the crystalline nanostructured material can be added at from about 0.05 to about 100 weight percent to the catalyst. The additive may be employed in chemical processing operations including, for example, catalytic cracking, fluidized catalytic cracking, hydrogenation, hydrosulfurization, hydrocracking, hydroisomerization, oligomerization, alkylation, or any of these in combination. For example, the addition of small amounts of fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites to conventional commercially available FCC catalysts allows for improvement in the catalytic performance.

Generally, FCC uses an FCC catalyst, which is typically a fine powder with a particle size of about 10 to 200 microns. The FCC catalyst can be suspended in the feed and propelled upward into a reaction zone. A relatively heavy hydrocarbon or petrochemical feedstock (e.g., a gas oil) can be mixed with the FCC catalyst to provide a fluidized suspension. The feed stock can be cracked in an elongated reactor, or riser, at elevated temperatures to provide a mixture of petrochemical products that are lighter hydrocarbon products than were provided in the feed stock. Gaseous reaction products and spent catalyst are discharged from the riser into a separator where they can be regenerated. Typical FCC conversion conditions employing FCC catalysts include a riser top temperature of about 500 to about 595° C., a catalyst/oil weight ratio of about 3 to about 12, and a catalyst residence time of about 0.5 to about 15 seconds. The higher activity of the mesostructured catalysts and/or the crystalline nanostructure catalyst can enable less severe processing conditions, such as, for example, lower temperature, lower catalyst to oil ratios, and/or lower contact time.

In various embodiments, a small amount of mesostructured material (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured material blended with conventional FCC catalysts can enable pre-cracking of the bulkier molecules by the mesostructured material and/or crystalline nanostructured material contained in the blend. Conventional FCC catalysts have pore sizes too small to accommodate bulkier molecules. After the bulkier molecules have been pre-cracked they are processed in the small pores of the conventional FCC catalyst.

FIG. 23 depicts MAT yield results where a fully crystalline mesostructured zeolite H—Y[MCM-41] was employed as an additive to a conventional unmodified zeolite H—Y for fluid catalytic cracking of a vacuum gas oil. The results from left to right on the x-axis show 100% H-Y with no additive, 10% H—Y[MCM-41] additive to the catalyst, 20% H—Y[MCM-41] additive to the catalyst, 50% H—Y[MCM-41] additive to the catalyst, and 100% H—Y[MCM-41]. MAT conditions include a reaction temperature of 500° C., catalyst contact time of 60 seconds, a catalyst charge of 1 gram, a catalyst-to-vacuum gas oil ratio of 2, and a WHSV of 30 g/h/g. In FIG. 23, the bar labeled LCO shows the yield of light cycle oil and the bar labeled HCO shows the yield of fractions heavier than gasoline.

Referring still to FIG. 23, the addition of the fully crystalline mesostructured zeolite to the conventional FCC catalyst produced a significant impact over the yield structure that does not correspond to the linear combination of both materials. The data suggests the pre-cracking effect of a fully crystalline mesostructured zeolite additive to a catalyst. A significant conversion improvement in the heavier fractions (“HCO”) was obtained at 10% fully crystalline mesostructured zeolite. The incremental amounts of fully crystalline mesostructured zeolites, 20% and 50%, does not produce an increase in gasoline production or conversion, and does not decrease the HCO as compared to the 10% additive quantity. This data supports the pre-cracking effect of the fully crystalline mesostructured zeolite additive. The higher amount of total dry gas, LPG, and coke produced when fully crystalline mesostructured zeolites as used as FCC additives may be due to the higher conversion obtained when the fully crystalline zeolite materials were employed. A similar pre-cracking effect can be expected where a crystalline nanostructure zeolite is employed as an additive.

In various embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructure materials can be blended with conventional catalysts. The additive mesostructured materials and/or crystalline nanostructure materials can be incorporated into the conventional catalyst pellet. Shaped (e.g., pelletized) mesostructured materials and/or crystalline nanostructure materials can be mixed with the catalyst pellet. Alternatively, a conventional catalyst and the mesostructured and/or nanostructured materials can be layered together. Any such mixture can be used in a refining application, for example, in fluidized catalytic cracking directly as is done with other additives, The amount of mesostructured zeolite added and the manner by which it is blended can be used to tune the yield and/or the structure of the products.

In one or more embodiments, the addition of or incorporation of mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials to conventional commercially available Thermofor Catalytic Cracking (“TCC”) catalysts provides an improvement in the catalytic performance. The TCC process is a moving bed process that uses pellet or bead shaped conventional catalysts having an average particle size of about one-sixty-fourth to one-fourth inch. Hot catalyst beads progress with a hydrocarbon or petrochemical feed stock downwardly through a cracking reaction zone. The hydrocarbon products are separated from the spent catalyst and recovered. The catalyst is recovered at the lower end of the zone and recycled (e.g., regenerated). Typically, TCC conversion conditions include an average reactor temperature from about 450 to about 510° C., a catalyst/oil volume ratio of from about 2 to about 7, and a reactor space velocity of from about 1 to about 2.5 vol/hr/vol. Mesostructured materials and/or crystalline nanostructured materials can be substituted for TCC catalysts to improve the catalytic cracking of petrochemical or hydrocarbon feed stocks to petroleum product. Alternatively, the mesostructured materials and/or crystalline nanostructured materials can be blended with the TCC catalyst.

In various embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used as catalyst additives in any other catalytic application. For example, they may be used as additives in processes where bulky molecules must be processed.

In other various embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used in hydrogenation. Conventional zeolites are good hydrogenation supports because they possess a level of acidity needed both for the hydrogenation of the aromatic compounds and for tolerance to poisons such as, for example, sulfur. However, the small pore size of conventional zeolites limit the size of the molecules that can be hydrogenated. Various metals, such as Pt, Pd, Ni, Co, Mo, or mixtures of such metals, can be supported on mesostructured materials using surface modification methods, for example, ion exchange, described herein. The hydrogenation catalytic activity of mesostructured materials modified to support various metals (e.g., doped with metals) shows a higher hydrogenation activity for bulky aromatic compounds as compared to other conventional materials, for example, metal supported on alumina, silica, metal oxides, MCM-41, and conventional zeolites. The mesostructured materials modified to support various metals also show, compared to conventional materials, a higher tolerance to sulfur, for example, sulfur added as thiophene and dibenzothiophene, which are common bulky components of crude oil that often end up in gas oil fractions.

In other various embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used in hydrodesulfurization (“HDS”), including, for example, deep HDS, hydrodesulfurization of 4,6-dialkyldibenzothiophenes, Deep removal of sulfur species from gas oil has two main limitations: i) the very low reactivity of some sulfur species, for example, dimethyldibenzothiophenes and ii) the presence of inhibitors in the feed stocks such as, for example, H₂S. Deep HDS is currently done with active metal sulfides on alumina, silica/alumina, and alumina/zeolite.

Generally, during HDS the feed stock is reacted with hydrogen in the presence of an HDS catalyst. Oxygen and any sulfur and nitrogen present in the feed is reduced to low levels. Aromatics and olefins are also reduced. The HDS reaction conditions are selected to minimize cracking reactions, which reduce the yield of the most desulfided fuel product. Hydrotreating conditions typically include a reaction temperature from about 400 to about 900° F., a pressure between 500 to 5,000 psig, a feed rate (LHSV) of 0.5 hr⁻¹ to 20 h⁻¹ (v/v), and overall hydrogen consumption of 300 to 2,000 scf per barrel of liquid hydrocarbon feed (53.4-356 m³ H₂/m³ feed).

Suitable active metal sulfides include, for example, Ni and Co/Mo sulfides. Zeolites provide strong acidity, which improves HDS of refractory sulfur species through methyl group migration. Zeolites also enhance the hydrogenation of neighboring aromatic rings. Zeolite acidity enhances the liberation of H₂S from the metal sulfide increasing the tolerance of the catalyst to inhibitors. However, bulky methylated polyaromatic sulfur species are not able to access the acidic sites of conventional zeolites. In contrast, the controlled mesoporosity and strong acidity of fully crystalline mesostructured zeolites provide accessibility to the acidic sites and acidity that allows for the deeper HDS required for meeting future environmental restrictions.

In other various embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used in hydrocracking. Metals, including noble metals such as, for example, Ni, Co, W, and Mo, and metal compounds are commercially used in hydrocracking reactions. These metals can be supported on mesostructured materials by previously described methods. The mesostructured materials including metals can be employed for hydrocracking of various feedstocks such as, for example, petrochemical and hydrocarbon feed materials.

Typically, hydrocracking involves passing a feed stock (i.e., a feed material), such as the heavy fraction, through one or more hydrocracking catalyst beds under conditions of elevated temperature and/or pressure. The plurality of catalyst beds may function to remove impurities such as any metals and other solids. The catalyst beads also crack or convert the longer chain molecules in the feedstock into smaller ones. Hydrocracking can be effected by contacting the particular fraction or combination of fractions with hydrogen in the presence of a suitable catalyst at conditions, including temperatures in the range of from about 600 to about 900° F. and at pressures from about 200 to about 4,000 psia, using space velocities based on the hydrocarbon feedstock of about 0.1 to 10 hr⁻¹.

As compared to conventional unmodified catalyst supports such as, for example, alumina, silica, and zeolites, the mesostructured materials including metals allow for the hydrocracking of higher boiling point feed materials. The mesostructured materials including metals produce a low concentration of heteroatoms and a low concentration of aromatic compounds. The mesostructured materials including metals exhibit bifunctional activity. The metal, for example a noble metal, catalyzes the dissociative adsorption of hydrogen and the mesostructured material provides the acidity.

The controlled pore size and controlled mesopore surface in the mesostructured materials including metals can make the bifunctional activity more efficiently present in the mesostructured catalysts as compared to a bifunctional conventional catalyst. In addition to the zeolitic acidity present in the fully crystalline mesostructured zeolites, the controlled pore size enables larger pores that allow for a high dispersion of the metal phase and the processing of large hydrocarbons.

In other embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used in hydroisomerization. Various metals and mixtures of metals, including, for example, noble metals such as nickel or molybdenum and combinations thereof in, for example, their acidic form, can be supported on mesostructured materials.

Typically, hydroisomerization is used to convert linear paraffins to branched paraffins in the presence of a catalyst and in a hydrogen-rich atmosphere. Hydroisomerization catalysts useful for isomerization processes are generally bifunctional catalysts that include a dehydrogenation/hydrogenation component and an acidic component. Paraffins were exposed to fully crystalline mesostructured zeolites including metals and were isomerized in a hydrogen flow at a temperature ranging from about 150 to about 350° C. thereby producing branched hydrocarbons and high octane products. The fully crystalline mesostructured zeolites including metals permit hydroisomerization of bulkier molecules than is possible with commercial conventional catalysts due, at least in part, to their controlled pore size and pore volume.

In other embodiments, mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used in the oligomerization of olefins. The controlled pore shape, pore size, and pore volume improves the selectivity properties of the mesostructured materials. The selectivity properties, the increased surface area present in the mesospore surfaces, and the more open structure of the mesostructured materials can be used to control the contact time of the reactants, reactions, and products inside the mesostructured materials. The olefin can contact the mesostructured materials at relatively low temperatures to produce mainly middle-distillate products via olefin-oligomerization reactions. By increasing the reaction temperature, gasoline can be produced as the primary fraction.

Where the mesostructured materials are used in FCC processes, the yield of olefins production can be increased relative to FCC with conventional zeolites. The increased yield of olefins can be reacted by oligomerization in an olefin-to-gasoline-and/or-diesel process, such as, for example, MOGD (Mobile Olefins to Gas and Diesel, a process to convert olefins to gas and diesel). In addition, olefins of more complex structure can be oligomerized using the mesostructured materials described herein.

The LPG fraction produced using mesostructured materials has a higher concentration of olefins compared to other catalysts, including, for example, various conventional FCC catalysts, zeolites, metals oxides, and clays under catalytic cracking conditions both in fixed bed and fluidized bed reactor conditions. The mesopore size of the mesostructured materials readily allows the cracked products to exit the mesostructured materials. Accordingly, hydrogen transfer reactions are reduced and the undesired transformation of olefins to paraffins in the LPG fraction is reduced. In addition, over-cracking and coke formation are limited, which increases the average life time of the catalyst.

The controlled pore size, pore volume, and mesopore surfaces provide an open structure in the mesostructured materials. This open structure reduces the hydrogen transfer reactions in the gasoline fraction and limits the undesired transformation of olefins and naphthenes into paraffins and aromatics. As a result, the octane number (both RON and MON) of the gasoline produced using the mesostructured materials is increased.

The acidity and the controlled mesoporosity present in the mesostructured materials can enable their use in alkylation reactions. Specifically, olefins and paraffins react in the presence of the mesostructured materials to produce highly branched octanes. The highly branched octane products readily exit the open structure of the fully crystalline mesostructured materials, thereby minimizing unwanted olefin oligomerization.

In other embodiments, the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used to process a petrochemical feed material to petrochemical product by employing any of a number of shape selective petrochemical and/or hydrocarbon conversion processes. In one embodiment, a petrochemical feed can be contacted with the mesostructured material under reaction conditions suitable for dehydrogenating hydrocarbon compounds. Generally, such reaction conditions include, for example, a temperature of from about 300 to about 700° C., a pressure from about 0.1 to about 10 atm, and a WHSV from about 0.1 to about 20 hr⁻¹.

In other embodiments, a petrochemical feed can be contacted with the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials under reaction conditions suitable for converting paraffins to aromatics. Generally, such reaction conditions include, for example, a temperature of from about 300 to about 700° C., a pressure from about 0.1 to about 60 atm, a WHSV of from about 0.5 to about 400 hr⁻¹, and an H₂/HC mole ratio of from about 0 to about 20.

In other embodiments, a petrochemical feed can be contacted with the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials under reaction conditions suitable for converting olefins to aromatics. Generally, such reaction conditions include, for example, a temperature of from about 100 to about 700° C., a pressure from about 0.1 to about 60 atm, a WHSV of from about 0.5 to about 400 hr⁻¹, and an H₂/HC mole ratio from about 0 to about 20.

In other embodiments, a petrochemical feed can be contacted with the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials under reaction conditions suitable for isomerizing alkyl aromatic feedstock components. Generally, such reaction conditions include, for example, a temperature of from about 230 to about 510° C., a pressure from about 3 to about 35 atm, a WHSV of from about 0.1 to about 200 hr⁻¹ and an H₂/HC mole ratio of from about 0 to about 100.

In other embodiments, a petrochemical feed can be contacted with the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials under reactions conditions suitable for disproportionating alkyl aromatic components. Generally, such reaction conditions include, for example, a temperature ranging from about 200 to about 760° C., a pressure ranging from about 1 to about 60 atm, and a WHSV of from about 0.08 to about 20 hr⁻¹.

In other embodiments, a petrochemical feed can be contacted with the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials under reaction conditions suitable for alkylating aromatic hydrocarbons (e.g., benzene and alkylbenzenes) in the presence of an alkylating agent (e.g., olefins, formaldehyde, alkyl halides and alcohols). Generally, such reaction conditions include a temperature of from about 250 to about 500° C., a pressure from about 1 to about 200 atm, a WHSV of from about 2 to about 2,000 hr⁻¹, and an aromatic hydrocarbon/alkylating agent mole ratio of from about 1/1 to about 20/1.

In other embodiments, a petrochemical feed can be contacted with the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials under reaction conditions suitable for transalkylating aromatic hydrocarbons in the presence of polyalkylaromatic hydrocarbons. Generally, such reaction conditions include, for example, a temperature of from about 340 to about 500° C., a pressure from about 1 to about 200 atm, a WHSV of from about 10 to about 1,000 hr⁻¹, and an aromatic hydrocarbon/polyalkylaromatic hydrocarbon mole ratio of from about 1/1 to about 16/1.

Generally, suitable conditions for a petrochemical or hydrocarbon feed to contact the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials include temperatures ranging from about 100 to about 760° C., pressures ranging from above 0 to about 3,000 psig, a WHSV of from about 0.08 to about 2,000 hr⁻¹, and a hydrocarbon compound mole ratio of from 0 to about 100.

Application in Compound Removal

The microporosity, mesoporosity, and ion exchange properties present in the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or in crystalline nanostructured materials can enable removal of inorganic and organic compounds from solutions. Suitable solutions can be aqueous or organic solutions. Accordingly, the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be employed in water treatment, water purification, pollutant removal, and/or solvent drying.

For example, 1 gram of Na⁺ and a fully crystalline mesostructured zeolite is suspended in 1 L of a methylene blue aqueous solution, stirred for 12 hours, and filtered. The fully crystalline mesostructured zeolite removes the methylene blue from the aqueous solution. Other configurations such as fixed bed, filters, and membranes can be also used in addition to the mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials. Optionally, fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be employed as additives with conventional separation means, for example, fixed bed, filters, and membranes. The fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be substituted for other separation means in, for example, fixed bed, filters, and membranes. The fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be recycled by ion exchange, drying, calcinations or other conventional techniques and reused.

Application in Adsorption

The mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or crystalline nanostructured materials can be used to adsorb gaseous compounds including, for example, volatile organic compounds (“VOCs”), which are too bulky to be adsorbed by conventional unmodified zeolites. Accordingly, pollutants that are too bulky to be removed by conventional unmodified zeolites can be removed from a gaseous phase by direct adsorption. When the mesostructured or nanostructured material is a zeolite, the fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be employed for adsorption in various adsorption configurations such as, for example, membranes, filters and fixed beds. Adsorbed organic compounds can be desorbed from the fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites by heat treatment. Thus, the fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be recycled and then reused.

Application in Gas Separation

Fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be grown on various supports by employed techniques such as, for example, seeding, hydrothermal treatment, dip coating, and/or use of organic compounds. They can be physically mixed with conventional zeolites or metal oxides. Continuous layers of fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites can be used as membranes and/or catalytic membranes on, for example, porous supports.

Fully crystalline mesostructured zeolites and/or crystalline nanostructured zeolites are unique molecular sieves containing both microporosity and mesoporosity. They may be employed in various configurations including, for example, membranes for separation of gases based on physicochemical properties such as, for example, size, shape, chemical affinity, and physical properties.

Application in Fine Chemicals and Pharmaceuticals

A fully crystalline mesostructured zeolite has increased active site accessibility as compared to the same zeolite in conventional form. Similarly, crystalline nanostructure zeolites have increased active site accessibility compared to the same zeolite in conventional form. Accordingly, the activity of some important chemical reactions used in fine chemical and pharmaceutical production can be improved by substituting a conventional zeolite used in the process for a fully crystalline mesostructured zeolite and/or a crystalline nanostructure zeolite. In addition, a fully crystalline mesostructured zeolite and/or a crystalline nanostructure zeolite may be employed as an additive to a catalyst typically employed in such fine chemical and pharmaceutical production reactions. Suitable processes that can be improved by using a fully crystalline mesostructured zeolite and/or a crystalline nanostructure zeolite include, for example, isomerization of olefins, isomerization of functionalized saturated systems, ring enlargement reactions, Beckman rearrangements, isomerization of arenes, alkylation of aromatic compounds, acylation of arenes, ethers, and aromatics, nitration and halogenation of aromatics, hydroxyalylation of arenes, carbocyclic ring formation (including Diels-Alder cycloadditions), ring closure towards heterocyclic compounds, amination reactions (including amination of alcohols and olefins), nucleophilic addition to epoxides, addition to oxygen-compounds to olefins, esterification, acetalization, addition of heteroatom compounds to olefins, oxidation/reduction reactions such as, but not limited to, Meerwein-Ponndorf-Verley reduction and Oppenauer oxidation, dehydration reactions, condensation reactions, C—C formation reactions, hydroformylation, acetilization, and amidation.

Application in Slow Release Systems

Chemicals and/or materials having useful properties such as, for example, drugs, pharmaceuticals, fine chemicals, optic, conducting, semiconducting magnetic materials, nanoparticles, or combinations thereof, can be introduced to mesostructured materials (e.g., fully crystalline mesostructured zeolites) and/or a crystalline nanostructured materials using one or more of the modifying methods described herein. For example, chemicals and/or materials may be incorporated into the mesostructured materials by, for example, adsorption or ion exchange. In addition, such useful chemicals can be combined with the mesostructured materials and/or crystalline nanostructure materials by creating a physical mixture, a chemical reaction, heat treatment, irradiation, ultrasonication, or any combination thereof.

The release of the chemicals and/or materials having useful properties can be controlled. Controlled release may take place in various systems such as, for example, chemical reactions, living organisms, blood, soil, water, and air. The controlled release can be accomplished by physical reactions or by chemical reactions. For example, controlled release can be accomplished by chemical reactions, pH variation, concentration gradients, osmosis, heat treatment, irradiation, and/or magnetic fields.

Kits

One or more embodiments also provide kits for conveniently and effectively implementing various methods described herein. Such kits can comprise any of the mesostructured and/or nanostructured materials (e.g., zeolitic structures) described herein, and a means for facilitating their use consistent with various methods. Such kits may provide a convenient and effective means for assuring that the methods are practiced in an effective manner. The compliance means of such kits may include any means that facilitate practicing one or more methods associated with the materials described herein. Such compliance means may include instructions, packaging, dispensing means, or combinations thereof. Kit components may be packaged for either manual or partially or wholly automated practice of the foregoing methods. In other embodiments involving kits, a kit is contemplated that includes block copolymers, and optionally instructions for their use.

EXAMPLES

Example 1

Pretreatment and Riving of ZSM-5 Zeolite with Silica-to-Alumina Ratio of 23

40 grams of NH₄-ZSM-5 having a silica-to-alumina ratio (“SAR”) of 23 was heated at 900° C. for 1 hour. The cooled product was treated with 0.19 mL of 50% NaOH solution, 0.5 g of cetyltrimethylammonium bromide (“CTAB”), and 4 g of water per gram of zeolite (hydrated) at 80° C. for 4 hours. The product was washed three times with hot (−80° C.) water and dried. This material was exchanged twice at 25° C. with 10 mL of 2N NH₄NO₃ per gram of product, with stirring, for 30 minutes. The product was calcined in flowing nitrogen gas for 1 hour at 600° C., cooled to 300° C., heated in flowing dry air to 600° C., and held at 600° C. for 2 hours. The product was characterized via x-ray diffraction, temperature programmed ammonia desorption (“TPAD”) for acidity, and argon gas adsorption for micropore and mesopore volume. This process was repeated for a second sample except using an initial heating temperature of 825° C. Following analysis, each sample was subjected to steam treatment at 788° C. to determine crystallinity stability. The results, given in Table 1 below, demonstrate the effect of temperature during pretreatment on the generation of mesopore volume, showing an increase in mesoporosity at 900° C. over 825° C. Each of these materials exhibited good crystallinity before and after steaming.

TABLE 1
Mesoporosity of Pretreated Zeolites
	Pore Size Range (Å)
Sample:	0-20	20-80	80-120	80-200	80-500
AC900	0.144 cc/g	0.086 cc/g	0.029 cc/g	0.048 cc/g	0.071 cc/g
(pre-steam)
AC900	0.144 cc/g	0.023 cc/g	0.034 cc/g	0.063 cc/g	0.109 cc/g
(post-steam)
AC825	0.200 cc/g	0.042 cc/g	0.021 cc/g	0.035 cc/g	0.053 cc/g
(pre-steam)
AC825	0.177 cc/g	0.023 cc/g	0.041 cc/g	0.052 cc/g	0.075 cc/g
(post-steam)

Example 2

Pretreatment and Riving of ZSM-5 Zeolite with Silica-to-Alumina Ratio of 23

40 grams of NH₄-ZSM-5 having a SAR of 23 were heated at 900° C. for 1 hour. The cooled product was treated with 0.03 mL of 50% NaOH solution, 0.5 g of CTAB, and 4 g of water per gram of zeolite (hydrated) at 80° C. for 4 hours. The product was washed three times with hot (−80° C.) water and dried. This material was exchanged twice at 80° C. with 10 mL of 2N NH₄NO₃ per gram of product, with stirring, for 60 minutes. The product was calcined in flowing nitrogen gas for 1 hour at 600° C., cooled to 300° C., heated in flowing dry air to 600° C., and held at 600° C. for 2 hours. The product was characterized via x-ray diffraction, temperature programmed ammonia desorption (“TPAD”) for acidity, and argon gas adsorption for micropore and mesopore volume.

This process was repeated for NaOH addition amounts of 0.0, 0.06, 0.09 and 0.12 mL per gram of zeolite. The results, given in Table 2 below, demonstrate controlled generation of mesopore volume with increasing amounts of added 50% NaOH solution.

Example 3

Pretreatment and Riving of ZSM-5 Zeolite with Silica-to-Alumina Ratio of 50

120 grams of NH₄-ZSM-5 having a SAR of 50 were heated at 900° C. for 1 hour. The cooled product was treated with 0.08 g of 50% NaOH solution, 0.5 g of CTAB, and 4 g of water per gram of zeolite (hydrated) at 80° C. for 4 hours. The product was washed three times with hot (−80° C.) water and dried. The resulting material was exchanged twice at 80° C. with 10 mL of 2N NH₄NO₃ per gram of product, with stirring, for 60 minutes. The product was calcined in flowing nitrogen gas for 1 hour at 600° C., cooled to 300° C., heated in flowing dry air to 600° C., and held at 600° C. for 2 hours. The product was characterized via x-ray diffraction, temperature programmed ammonia desorption (“TPAD”) for acidity, and argon gas adsorption for micropore and mesopore volume.

This process was repeated for NaOH addition amounts of 0.0, 0.14, 0.20, 0.25 and 0.30 g per gram of zeolite. The results, given in Table 2 below, demonstrate controlled generation of mesopore volume with increasing amounts of added 50% NaOH solution.

Example 4

Pretreatment and Riving of ZSM-5 Zeolite with Silica-to-Alumina Ratio of 80

120 grams of NH₄-ZSM-5 having a SAR of 80 were heated at 900° C. for 1 hour. The cooled product was treated with 0.08 g of 50% NaOH solution, 0.5 g of CTAB, and 4 g of water per gram of zeolite (hydrated) at 80° C. for 4 hours. The resulting product was washed three times with hot (−80° C.) water and dried. This material was exchanged twice at 80° C. with 10 mL of 2N NH₄NO₃ per gram of product, with stirring, for 60 minutes. The product was calcined in flowing nitrogen gas for 1 hour at 600° C., cooled to 300° C., heated in flowing dry air to 600° C., and held at 600° C. for 2 hours. The product was characterized via x-ray diffraction, temperature programmed ammonia desorption (“TPAD”) for acidity, and argon gas adsorption for micropore and mesopore volume.

This process was repeated for NaOH addition amounts of 0.0, 0.14, 0.20, 0.25 and 0.30 g per gram of zeolite. The results, given in Table 2 below, demonstrate controlled generation of mesopore volume with increasing amounts of added 50% NaOH solution.

TABLE 2
Variation of NaOH/Zeolite and Si/Al Ratios
				Micropore	Mesopore
	Si/Al	g NaOH/		Volume	Volume
Sample	Ratio	g Zeolite	Crystallinity	(0-20 Å)	(20-300 Å)
ZSM-5	80	0.00	90	0.21 cc/g	0.08 cc/g
(80)	80	0.08	90	0.21 cc/g	0.11 cc/g
	80	0.14	90	0.21 cc/g	0.17 cc/g
	80	0.20	82	0.18 cc/g	0.24 cc/g
	80	0.25	81	0.19 cc/g	0.32 cc/g
	80	0.30	70	0.19 cc/g	0.42 cc/g
ZSM-5	50	0.00	88	0.20 cc/g	0.07 cc/g
(50)	50	0.08	89	0.20 cc/g	0.08 cc/g
	50	0.14	86	0.20 cc/g	0.17 cc/g
	50	0.20	81	0.20 cc/g	0.20 cc/g
	50	0.25	77	0.19 cc/g	0.26 cc/g
	50	0.30	70	0.16 cc/g	0.32 cc/g
ZSM-5	23	0.00**	100	0.233 cc/g	0.045 cc/g
(23)	23	0.03*	80	0.190 cc/g	0.050 cc/g
	23	0.06*	71	0.186 cc/g	0.077 cc/g
	23	0.09*	63	0.171 cc/g	0.119 cc/g
	23	0.12*	54	0.135 cc/g	0.177 cc/g
*mL per gram of zeolite
**Not rived or pre-calcined

Example 5

Pretreatment Steaming and Riving of ZSM-5 Zeolite with Silica to Alumina Ratio of 23

100 grams of NH₄-ZSM-5 having a SAR of 23 were heated in a 100% steam atmosphere at 800° C. for 2 hours. The cooled product was treated with 0.15 g of 50% NaOH solution, 0.5 g of CTAS, and 4 g of water per gram of zeolite (hydrated) at 80° C. for 4 hours. The resulting product was washed three times with hot (−80° C.) water and dried. This material was exchanged twice at 80° C. with 10 mL of 2N NH₄NO₃ per gram of product, with stirring, for 30 minutes. The product was calcined in flowing nitrogen gas for 1 hour at 600° C., cooled to 300° C., heated in flowing dry air to 600° C., and held at 600° C. for 2 hours. The product was characterized via x-ray diffraction, temperature programmed ammonia desorption (“TPAD”) for acidity, and argon gas adsorption for micropore and mesopore volume.

This process was repeated for a steaming time of 1 hour, using 50 g dry zeolite, and with NaOH addition amounts of 0.25 and 0.35 g per gram of zeolite. The results, given in Table 3 below, demonstrate that presteaming at 800° C. results in controlled generation of mesopore volume with amount of added 50% NaOH solution.

TABLE 3
Effect of NaOH Level on Mesopore
Formation of Presteamed ZSM-5
	SiO2/			Micropore	Mesopore
	Al2O3	g NaOH/		Volume	Volume
Sample	Ratio	g Zeolite	Crystallinity	(0-20 Å)	(20-300 Å)
ZSM-5	23**	—	100	0.233 cc/g	0.045 cc/g
(23)	23	0.15	70	0.170 cc/g	0.098 cc/g
	23	0.25	50*	0.103 cc/g	0.452 cc/g
	23	0.35	51*	0.108 cc/g	0.385 cc/g
*Estimated from micropore volume value.
**Not rived or pre-calcined

Comparative Example 6

Riving of ZSM-5(23) Without Pretreatment

100 g of NH₄-ZSM-5 with a silica-to-alumina ratio of 23 were contacted with 316 g of water, 9.38 g of NaOH, and 50 grams of CTAB. After thorough mixing it was heated at 80° C. for 16 hours. After filtering and washing, argon adsorption measurements indicated 0.16 and 0.045 cc/g of micro- and mesopore volume respectively, in the 0-20 and 20-300 Å diameter range, revealing little, if any, formation of mesopores.

Comparative Example 7

Riving of ZSM-5(23) Without Pretreatment

1,000 g of ZSM-5 with a silica-to-alumina ratio of 23 were contacted with 1,832 g of water and 500 g of CTAB and mixed at 78-80° C. for 15 minutes. To this slurry, 376 g of NaOH was added and mixed for 15 minutes. It was then allowed to stand at this temperature for 16 hours (overnight). It was then given two exchanges. For the first 625 g of ZSM-5 product, 2,292 g of water and 181 g of NH₄NO₃ was stirred 30 minutes at 76-80° C. For the second exchange, 530 g of ZSM-5 was contacted with 1,943 g of water and 153 g of NH₄NO₃ for 30 minutes at 76-80° C. Argon adsorption measurements indicated 0.184 and 0.065 cc/g of micropore and mesopore volume in the 0-20 and 20-300 Å range, respectively. As with comparative example 6, little, if any, mesopores were formed employing this process.

SELECTED DEFINITIONS

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

As used herein, the terms “a,” “an,” and “the” mean one or more.

As used herein, the term “and/or,” when used in a list of two or more items, means that any one of the listed items can be employed by itself or any combination of two or more of the listed items can be employed. For example, if a composition is described as containing components A, B, and/or C, the composition can contain A alone; B alone; C alone; A and B in combination; A and C in combination, B and C in combination; or A, 13, and C in combination.

The term “catalyst” is art-recognized and refers to any substance that notably affects the rate of a chemical reaction without itself being consumed or significantly altered.

The term “cracking” is art-recognized and refers to any process of breaking up organic compounds into smaller molecules.

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

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

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

The term “including” is used to mean “including but not limited to.” “Including” and “including but not limited to” are used interchangeably.

“MCM-41” refers to a Mobil composite of matter that is an amorphous mesoporous silica with a hexagonal pore arrangement, where the mean pore diameter is in the range of about 2 to 10 nm.

“MCM-48” refers to a Mobil composite of matter that is an amorphous mesoporous silica with a cubic pore arrangement, where the mean pore diameter is in the range of about 2 to 10 nm.

“MCM-50” refers to a Mobil composite of matter that is an amorphous mesoporous silica with a lamellar pore arrangement, where the mean pore diameter is in the range of about 2 to 10 nm.

The term “mesoporous” is art-recognized and refers to a porous material comprising pores with an intermediate size, ranging anywhere from about 2 to about 60 nanometers (20 to 600 angstroms).

The term “mesostructure” is art-recognized and refers to a structure comprising mesopores which control the architecture of the material at the mesoscopic or nanometer scale, including ordered and non-ordered mesostructured materials, as well as nanostructured materials (i.e., materials in which at least one of their dimension is in the nanometer size range) such as nanotubes, nanorings, nanorods, nanowires, nanoslabs, and the like.

The term “mesostructured zeolites” as used herein includes all crystalline mesoporous materials, such as zeolites, aluminophosphates, gallophosphates, zincophosphates, titanophosphates, etc. A mesostructured zeolite may be in the form of ordered mesporosity (as in, for example MCM-41, MCM-48 or SBA-15), non-ordered mesoporosity (as in mesocellular foams (“MCF”)), or mesoscale morphology (as in nanorods and nanotubes). The notation zeolite[mesostructure] is used to designate the different types of mesostructured zeolites.

“MOR” refers to mordenite, which is a zeolite comprising approximately 2 moles of sodium and potassium and approximately 1 mole of calcium in its orthorhombic crystal structure. This term also includes the acidic form of MOR which may also be represented as “H-MOR.”

“MSU-S (MFI)” represents a mesoporous material made with zeolites with a pore range of about 2-15 nm. The (MFI) refers to its structure.

“MSU-S (BEA)” represents a mesoporous material made with zeolites with a pore range of about 1-15 nm. The (BEA) refers to its structure.

“PNA” represents a semicrystallized form of MCM-41.

“SBA-15” represents mesoporous (alumino) silicas with pore diameters up to 30 nm arranged in a hexagonal manner and pore walls up to 6 nm thick.

The term “surfactant” is art-recognized and refers to any surface-active agent or substance that modifies the nature of surfaces, often reducing the surface tension of water. Cetyltrimethylammonium bromide is a non-limiting example of a surfactant.

“Y” represents a faujasite type zeolite. This term also includes the acidic form of Y which may also be represented as “H—Y.”

The term “zeolite” is defined as in the International Zeolite Association Constitution (Section 1.3) to include both natural and synthetic zeolites as well as molecular sieves and other macroporous and mesoporous materials having related properties and/or structures. The term “zeolite” also refers to a group, or any member of a group, of structured aluminosilicate minerals comprising cations such as sodium and calcium or, less commonly, barium, beryllium, lithium, potassium, magnesium and strontium; characterized by the ratio (Al+Si):O=approximately 1:2, an open tetrahedral framework structure capable of ion exchange, and loosely held water molecules that allow reversible dehydration. The term “zeolite” also includes “zeolite-related materials” or “zeotypes” which are prepared by replacing Si⁴⁺ or Al³⁺ with other elements as in the case of aluminophosphates (e.g., MeAPO, SAPO, ElAPO, MeAPSO, and ElAPSO), gallophosphates, zincophophates, titanosilieates, etc.

“ZSM-5” or “ZSM-5 (MFI)” represents a Mobil synthetic zeolite-5. This term also includes the acidic form of ZSM-5 which may also be represented as “H-ZSM-5.” The (MFI) relates to its structure.

A comprehensive list of the abbreviations utilized by organic chemists of ordinary skill in the art appears in the first issue of each volume of the Journal of Organic Chemistry; this list is typically presented in a table entitled Standard List of Abbreviations.

Contemplated equivalents of the zeolitic structures, subunits and other compositions described above include such materials which otherwise correspond thereto, and which have the same general properties thereof (e.g., biocompatible), wherein one or more simple variations of substituents are made which do not adversely affect the efficacy of such molecule to achieve its intended purpose.

Numerical Ranges

The present description uses numerical ranges to quantify certain parameters relating to the invention. It should be understood that when numerical ranges are provided, such ranges are to be construed as providing literal support for claim limitations that only recite the lower value of the range as well as claim limitations that only recite the upper value of the range. For example, a disclosed numerical range of 10 to 100 provides literal support for a claim reciting “greater than 10” (with no upper bounds) and a claim reciting “less than 100” (with no lower bounds).

The present description uses specific numerical values to quantify certain parameters relating to the invention, where the specific numerical values are not expressly part of a numerical range. It should be understood that each specific numerical value provided herein is to be construed as providing literal support for a broad, intermediate, and narrow range. The broad range associated with each specific numerical value is the numerical value plus and minus 60 percent of the numerical value, rounded to two significant digits. The intermediate range associated with each specific numerical value is the numerical value plus and minus 30 percent of the numerical value, rounded to two significant digits. The narrow range associated with each specific numerical value is the numerical value plus and minus 15 percent of the numerical value, rounded to two significant digits. For example, if the specification describes a specific temperature of 62° F., such a description provides literal support for a broad numerical range of 25° F. to 99° F. (62° F.+/−37° F.), an intermediate numerical range of 43° F. to 81° F. (62° F.+/−19° F.), and a narrow numerical range of 53° F. to 71° F. (62° F.+/−9° F.). These broad, intermediate, and narrow numerical ranges should be applied not only to the specific values, but should also be applied to differences between these specific values. Thus, if the specification describes a first pressure of 110 psia and a second pressure of 48 psia (a difference of 62 psi), the broad, intermediate, and narrow ranges for the pressure difference between these two streams would be 25 to 99 psi, 43 to 81 psi, and 53 to 71 psi, respectively.

Claims not Limited to Disclosed Embodiments

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

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

Claims

1. A method of preparing a mesoporous inorganic material, said method comprising: (a) treating at least one initial inorganic material for a period of time in a dehydroxylation environment to thereby produce a dehydroxylated inorganic material; and(b) contacting said dehydroxylated inorganic material with at least one pH controlling agent to thereby produce said mesoporous inorganic material.

2. The method of claim 1 wherein said treating removes at least 10 percent of the acidic hydroxyl groups from the initial inorganic material.

3. The method of claim 1 wherein said treating removes at least 30 percent of the acidic hydroxyl groups from the initial inorganic material.

4. The method of claim 1 wherein said initial inorganic material comprises a zeolite.

5. The method of claim 4 wherein said zeolite has a silica-to-alumina ratio of at least 10.

6. The method of claim 4 wherein said zeolite is selected from the group consisting of ZSM-5, ZSM-12, ZSM-22, beta zeolite, synthetic ferrierite (ZSM-35), synthetic mordenite, and mixtures of two or more thereof.

7. The method of claim 4 wherein said zeolite is ZSM-5.

8. The method of claim 1 wherein said time period of step (a) is at least 1 minute and said dehydroxylation environment has a temperature of at least 300° C.

9. The method of claim 1 wherein said dehydroxylation environment has a temperature in the range of from about 500 to about 1,200° C.

10. The method of claim 1 wherein said dehydroxylation environment comprises dried, flowing air in addition to said inorganic material, wherein said dehydroxylation environment comprises not more than 30 percent by volume of water.

11. The method of claim 1 wherein said pH controlling agent comprises a base.

12. The method of claim 11 wherein said contacting of step (b) comprises contacting said dehydroxylated inorganic material with a surfactant.

13. The method of claim 1 wherein said mesoporous inorganic material is mesostructured.

14. The method of claim 1 wherein said mesoporous inorganic material has a 20 to 300 Å diameter mesopore volume that is at least 5 percent greater than the 20 to 300 Å diameter mesopore volume of said initial inorganic material.

15. The method of claim 1 wherein said mesoporous inorganic material has a 20 to 300 Å diameter mesopore volume that is at least 0.02 cc/g greater than the 20 to 300 Å diameter mesopore volume of said initial inorganic material.

16. The method of claim 1 wherein said mesoporous inorganic material has a crystalline content that is at least 5 percent of the crystalline content of said initial inorganic material.

17. A method of preparing a mesoporous zeolite, said method comprising: (a) treating at least one zeolite for a period of time in a heat-treating environment having a temperature of at least 500° C. to thereby produce a heat-treated zeolite, wherein said heat-treating environment primarily comprises air and/or an inert gas in addition to said zeolite; and(b) contacting said heat-treated zeolite with at least one pH controlling agent to thereby produce said mesoporous zeolite.

18. The method of claim 17 wherein said treating removes at least 15 percent of the acidic hydroxyl groups from the zeolite.

19. The method of claim 17 wherein said zeolite has a silica-to-alumina ratio of at least 15.

20. The method of claim 17 wherein said zeolite is selected from the group consisting of ZSM-5, ZSM-12, ZSM-22, beta zeolite, synthetic ferrierite (ZSM-35), synthetic mordenite, and mixtures of two or more thereof.

21. The method of claim 17 wherein said zeolite is ZSM-5.

22. The method of claim 17 wherein said time period of step (a) is at least 1 minute and said heat-treating temperature is at least 700° C.

23. The method of claim 17 wherein said air and/or said inert gas is dried and flowing, wherein said dehydroxylation environment comprises not more than 30 percent by volume of water.

24. The method of claim 17 wherein said heat-treating environment comprises air in an amount of at least 70 percent by volume in addition to said zeolite.

25. The method of claim 17 wherein said pH controlling agent comprises a base.

26. The method of claim 25 wherein said contacting of step (b) comprises contacting said heat-treated zeolite with a surfactant.

27. The method of claim 17 wherein said mesoporous zeolite is mesostructured.

28. The method of claim 17 wherein said mesoporous zeolite has a 20 to 300 Å diameter mesopore volume that is at least 30 percent greater than the 20 to 300 Å diameter mesopore volume of said zeolite, wherein said mesoporous zeolite has a total 20 to 300 Å diameter mesopore volume of at least 0.05 cc/g.

29. The method of claim 17 wherein said mesoporous zeolite has a crystalline content that is at least 30 percent of the crystalline content of said zeolite.

30. A method of preparing a mesoporous zeolite, said method comprising: (a) contacting at least one zeolite with steam having a temperature of at least 300° C. for a period of time to thereby produce a steam-treated zeolite; and(b) contacting said steam-treated zeolite with at least one pH controlling agent to thereby produce said mesoporous zeolite.

31. The method of claim 30 wherein said contacting of step (a) removes at least 20 percent of the acidic hydroxyl groups from the zeolite.

32. The method of claim 30 wherein said zeolite has a silica-to-alumina ratio of at least 10.

33. The method of claim 30 wherein said zeolite is selected from the group consisting of ZSM-5, ZSM-12, ZSM-22, beta zeolite, synthetic ferrierite (ZSM-35), synthetic mordenite, and mixtures of two or more thereof.

34. The method of claim 30 wherein said zeolite is ZSM-5.

35. The method of claim 30 wherein said time period of step (a) is at least 1 minute and said steam has a temperature in the range of from about 400 to about 800° C.

36. The method of claim 30 wherein said pH controlling agent comprises a base.

37. The method of claim 36 wherein said contacting of step (b) comprises contacting said steam-treated zeolite with a surfactant.

38. The method of claim 30 wherein said mesoporous zeolite is mesostructured.

39. The method of claim 30 wherein said mesoporous zeolite has a 20 to 300 Å diameter mesopore volume that is at least 50 percent greater than the 20 to 300 Å diameter mesopore volume of said zeolite.

40. The method of claim 30 wherein said mesoporous zeolite has a crystalline content of at least 50 weight percent as measured by X-ray diffraction (“XRD”).