FIELD OF THE INVENTION

This invention relates to zeolite bound zeolite catalyst which can be tailored to optimize its performance and the use of the zeolite bound zeolite catalyst for hydrocarbon conversion processes.

BACKGROUND OF THE INVENTION

Crystalline microporous molecular sieves, both natural and synthetic, have been demonstrated to have catalytic properties for various types of hydrocarbon conversion processes. In addition, the crystalline microporous molecular sieves have been used as adsorbents and catalyst carriers for various types of hydrocarbon conversion processes, and other applications. These molecular sieves are ordered, porous, crystalline material having a definite crystalline structure as determined by x-ray diffraction, within which there are a large number of smaller cavities which may be interconnected by a number of still smaller channels or pores. The dimensions of these channels or pores are such as to allow for adsorption of molecules with certain dimensions while rejecting those of large dimensions. The interstitial spaces or channels formed by the crystalline network enable molecular sieves such as crystalline silicates, aluminosilicates, crystalline silicoalumino phosphates, and crystalline aluminophosphates, to be used as molecular sieves in separation processes and catalysts and catalyst supports in a wide variety of hydrocarbon conversion processes.

Within a pore of the crystalline molecular sieve, hydrocarbon conversion reactions such as paraffin isomerization, olefLn skeletal or double bond isomerization, disproportionation, alkylation, and transalkylation of aromatics are governed by constraints imposed by the channel size of the molecular sieve. Reactant selectivity occurs when a fraction of the feedstock is too large to enter the pores to react; while product selectivity occurs when some of the products can not leave the channels or do not subsequently react. Product distributions can also be altered by transition state selectivity in which certain reactions can not occur because the reaction transition state is too large to form within the pores. Selectivity can also result from configuration constraints on diffusion where the dimensions of the molecule approach that of the pore system. Non-selective reactions on the surface of the molecular sieve, such reactions on the surface acid sites of the molecular sieve, are generally not desirable as such reactions are not subject to the shape selective constraints imposed on those reactions occurring within the channels of the molecular sieve.

Zeolites are comprised of a lattice silica and optionally alumina combined with exchangeable cations such as alkali or alkaline earth metal ions. Although the term "zeolites" includes materials containing silica and optionally alumina, it is recognized that the silica and alumina portions may be replaced in whole or in part with other oxides. For example, germanium oxide, tin oxide, phosphorous oxide, and mixtures thereof can replace the silica portion. Boron oxide, iron oxide, gallium oxide, indium oxide, and mixtures thereof can replace the alumina portion. Accordingly, the terms "zeolite", "zeolites" and "zeolite material", as used herein, shall mean not only materials containing silicon and, optionally, aluminum atoms in the crystalline

lattice structure thereof, but also materials which contain suitable replacement atoms for such silicon and aluminum, such as gallosilicates, silicoaluminophosphates (SAPO) and aluminophosphates (ALPO). The term "aluminosilicate zeolite", as used herein, shall mean zeolite materials consisting essentially of silicon and aluminum atoms in the crystalline lattice structure thereof.

Synthetic zeolites are conventionally prepared by the crystallization of zeolites from a supersaturated synthesis mixture. The resulting crystalline product is then dried and calcined to produce a zeolite powder. Although the zeolite powder has good adsorptive properties, its practical applications are severely limited because it is difficult to operate fixed beds with zeolite powder. Therefore, prior to using the powder in commercial processes, the zeolite crystals are usually bound.

Mechanical strength is conventionally conferred on the zeolite provider by forming a zeolite aggregate such as a pill, sphere, or extrudate. The extrudate can be formed by extruding the zeolite in the presence of a non-zeolitic binder and drying and calcining the resulting extrudate. The binder materials used are resistant to the temperatures and other conditions, e.g., mechanical attrition, which occur in various hydrocarbon conversion processes. It is generally necessary that the zeolite be resistant to mechanical attrition, that is, the formation of fines which are small particles, e.g., particles having a size of less than 20 microns. Examples of suitable binders include amorphous materials such as alumina, silica, titania, and various types of clays.

Although such bound zeolite aggregates have much better mechanical strength than the zeolite powder, when the bound zeolite is used in a catalytic conversion process, the performance of the catalyst, e.g.,

activity, selectivity, activity maintenance, or combinations thereof, can be reduced because of the binder. For instance, since the binder is typically present in amounts of up to about 60 wt.% of zeolite, the binder dilutes the adsorptive properties of the zeolite aggregate. In addition, since the bound zeolite is prepared by extruding or otherwise forming the zeolite with the binder and subsequently drying and calcining the extrudate, the amorphous binder can penetrate the pores of the zeolite or otherwise block access to the pores of the zeolite, or slow the rate of mass transfer to and from the pores of the zeolite which can reduce the effectiveness of the zeolite when used in hydrocarbon conversion processes and other applications. Furthermore, when a bound zeolite is used in catalytic conversions processes, the binder may affect the chemical reactions that are taking place within the zeolite and also may itself catalyze undesirable reactions which can result in the formation of undesirable products. Therefore, it is desirable that zeolite catalysts used in hydrocarbon conversion not include deleterious amounts of such binders.

In certain hydrocarbon conversion processes, it is sometimes desirable that the catalyst used in the process be tailored to maximize its performance. For instance, it is sometimes desirable that the catalyst used in a hydrocarbon conversion process be a multifunctional catalyst, e.g., a bifunctional catalyst having the capability of performing two or more functions. A bifunctional catalyst comprises two separate catalysts which induce separate reactions. The reaction products can be separate or the two catalysts can be used together such that the reaction product of one catalyst is transported to and reacts on a catalyst site of the second catalyst. Also, since one of the benefits of using a zeolite catalyst is that the catalyst is shape selective and non- selective reactions on the surface of the zeolite are usually not

desirable, it is sometimes desirable that the catalyst used in a hydrocarbon conversion process have the capability of preventing or at least reducing unwanted reactions which may take place on the surface of the zeolite catalyst by selectively sieving molecules in the feedstream based on their size or shape to prevent undesirable molecules present in the feedstream from entering the catalytic phase of the zeolite catalyst and reacting with the catalyst. In addition, the performance of a zeolite catalyst can sometimes be maximized if the catalyst selectively sieves desired molecules based on their size or shape in order to prevent the molecules from exiting the catalyst phase of the catalyst.

The present invention provides a zeolite bound zeolite catalyst for use in hydrocarbon conversion processes which does not contain substantial amounts of a non-zeolitic binder and comprises core and binder zeolites that can be tailored to optimize its performance.

SUMMARY OF THE INVENTION

The present invention is directed to a zeohte bound zeohte catalyst which comprises first crystals of a first zeolite and a binder comprising second crystals of a second zeolite and the use of the zeolite bound zeolite catalyst in hydrocarbon conversion processes. The structure type of the second zeolite is different from the structure type of the first zeolite. The structure type of the first and second zeohtes and their composition, e.g. catalytic activity, are preferably tailored to provide a zeolite bound zeolite catalyst having enhanced performance. For example, the zeolite bound zeohte catalyst can be tailored to be multifunctional and/or can be tailored to prevent undesirable

molecules from entering or exiting the catalytic phase of the zeohte bound zeolite catalyst.

The zeohte bound zeohte catalyst of the present invention has application in hydrocarbon conversion processes and finds particular application in acid catalyzed reactions such as catalytic cracking, alkylation, dealkylation, disproportionation, and transalkylation reactions. In addition, the zeohte bound zeohte catalyst system of the present invention has particular application in other hydrocarbon conversion processes where cracking is not desired which include catalyzed reactions, such as, dehydrogenation, hydrocracking, isomerization, dewaxing, oligomerization, and reforming.

BRIEF DESCRIPTION OF THE DRAWINGS

Fig. 1 shows SEM micrographs of the product of Example 2.

Fig. 2 shows SEM micrographs of the product of Example 3.

DETAILED DESCRIPTION OF THE INVENTION

The present invention is directed to a zeohte bound zeohte catalyst and a process for converting organic compounds by contacting the organic compounds under conversion conditions with the zeohte bound zeohte catalyst. The zeohte bound zeohte catalyst comprises first crystals of a first zeohte and a binder comprising second crystals of a second zeohte. The structure type of the second zeohte is different from the structure type of the first zeohte. The use of the second crystals of a second zeohte as a binder results in a catalyst which provides a means for

controlling undesirable reactions taking place on or near the external surface of the first zeohte crystals and/or affects the mass transfer of hydrocarbon molecules to and from the pores of the first zeohte. Alternatively, the second zeohte binding crystals, if desired, can have catalytic activity, can function as a catalyst carrier, and/or can selectively prevent undesirable molecules from entering or exiting the pores of the first zeohte.

Unlike typical zeohte catalysts used in hydrocarbon conversion processes which are normally bound with sihca or alumina or other commonly used amorphous binders to enhance the mechanical strength of the zeohte, the zeohte catalyst of the present invention generally does not contain significant amounts of non-zeolitic binders. Preferably, the zeohte bound zeohte catalyst contains less than 10 percent by weight, based on the weight of the first and second zeohte, of non-zeolitic binder, more preferably contains less than 5 percent by weight, and, most preferably, the catalyst is substantially free of non- zeolitic binder. Preferably, the second zeohte crystals bind the first zeohte crystals by adhering to the surface of the first zeohte crystals thereby forming a matrix or bridge structure which also holds the first crystals particles together. More preferably, the second zeohte particles bind the first zeohte by intergrowing so as to form a coating or partial coating on the larger first zeohte crystals and, most preferably, the second zeohte crystals bind the first zeohte crystals by intergrowing to form an attrition resistant over-growth over the first zeohte crystals.

Although the invention is not intended to be hmited to any theory of operation, it is believed that one of the advantages of the zeohte bound zeohte catalyst of the present invention is obtained by the second

zeohte crystals controlling the accessibility of the acid sites on the external surfaces of the first zeohte to reactants. Since the acid sites existing on the external surface of a zeohte catalyst are not shape selective, these acid sites can adversely affect reactants entering the pores of the zeohte and products exiting the pores of the zeohte. In hne with this behef, since the acidity and structure type of the second zeohte can be carefully selected, the second zeohte does not significantly adversely affect the reactants exiting the pores of the first zeohte which can occur with conventionally bound zeohte catalysts and may beneficially affect the reactants exiting the pores of the first zeohte. Still further, since the second zeohte is not amorphous but, instead, is a molecular sieve, hydrocarbons may have increased access to the pores of the first zeohte during hydrocarbon conversion processes. Regardless of the theories proposed, the zeohte bound zeohte catalyst, when used in catalytic processes, has one or more of the improved properties which are disclosed herein.

The terms "acidity", 'lower acidity" and "higher acidity" as applied to zeohte are known to persons skilled in the art. The acidic properties of zeohte are well known. However, with respect to the present invention, a distinction must be made between acid strength and acid site density. Acid sites of a zeohte can be a Bronsted acid or a Lewis acid. The density of the acid sites and the number of acid sites are important in determining the acidity of the zeohte. Factors directly influencing the acid strength are (i) the chemical composition of the zeohte framework, i.e., relative concentration and type of tetrahedral atoms, (ii) the concentration of the extra -framework cations and the resulting extra-framework species, (hi) the local structure of the zeohte, e.g., the pore size and the location, within the crystal or at/near the surface of the zeohte, and (iv) the pretreatment conditions

and presence of co-adsorbed molecules. The amount of acidity is related to the degree of isomorphous substitution provided, however, such acidity is limited to the loss of acid sites for a pure Siθ2 composition. As used herein, the terms "acidity", 'lower acidity" and "higher acidity" refers to the concentration of acid sites irregardless of the strength of such acid sites which can be measured by ammonia absorption.

First and second zeohtes suitable for use in the zeohte bound zeohte catalyst of the present invention include large pore size zeohtes, intermediate pore size zeohtes, and small pore size zeohtes. These zeohtes are described in "Atlas of Zeohte Structure Types", eds. W. H. Meier and D.H. Olson, Butterworth-Heineman, Third Edition, 1992, which is hereby incorporated by reference. A large pore zeohte generally has a pore size greater than about 7 A and includes for example LTL, VFI, MAZ, MEI, FAU, EMT, OFF, BEA, and MOR structure type zeohtes (IUPAC Commission of Zeohte Nomenclature). Examples of large pore zeohtes, include, for example, mazzite, mordenite, offretite, zeohte L, VPI-5, zeohte Y, zeohte X, omega, Beta, ZSM-3, ZSM-4, ZSM-18, and ZSM-20. An intermediate pore size zeohte generally has a pore size from about δA, to about 7A and includes for example, MFI, MFS, MEL, MTW, EUO, MTT, HEU, FER, and TON structure type zeohtes (IUPAC Commission of Zeohte Nomenclature). Examples of intermediate pore size zeohtes, include ZSM-5, ZSM-12, ZSM-22, ZSM-23, ZSM-34, ZSM-35, ZSM-38, ZSM-48, ZSM-50, silicahte, and silicalite 2. A small pore size zeohte generally has a pore size from about 3A to about 5.θA and includes for example, CHA, ERI, KFI, LEV, and LTA structure type zeohtes (IUPAC Commission of Zeohte Nomenclature). Examples of small pore zeohtes

include ZK-4, ZK-14, ZK-21, ZK-22, ZK-5, ZK-20, zeohte A, erionite, chabazite, zeohte T, gemhnite, and chnoptilohte.

Preferred first and second zeohtes used in the zeohte bound zeohte catalyst comprise compositions which have the following molar relationship:

wherein X is a trivalent element, such as titanium, boron, aluminum, iron, and/or gallium, Y is a tetravalent element such as silicon, tin, and/or germanium, and n has a value of at least 2, said value being dependent upon the particular type of zeohte and the trivalent element present in the zeohte.

When either zeohte has intermediate pore size, the zeohte preferably comprises a composition having the following molar relationship:

wherein X is a trivalent element, such as aluminum, and/or gallium, Y is a tetravalent element such as silicon, tin, and/or germanium; and n has a value greater than 10, said value being dependent upon the particular type of zeohte and the trivalent element present in the zeohte. When the first or second zeohte has a MFI structure, n is preferably greater than 20.

As known to persons skilled in the art, the acidity of a zeohte can be reduced using many techniques such as by dealumination and steaming. In addition, the acidity of a zeohte is dependent upon the

form of the zeohte with the hydrogen form having the highest acidity and other forms of the zeohte such as the sodium form having less acidity than the acid form. Accordingly, the mole ratios of sihca to alumina and silica to gallia disclosed herein shall include not only zeohtes having the disclosed mole ratios, but shall also include zeohtes not having the disclosed mole ratios but having equivalent catalytic activity.

When the first zeohte is a gallium silicate intermediate pore size zeohte, the zeohte preferably comprises a composition having the following molar relationship:

Ga ₂ O ₃ :ySiO ₂

wherein y is between about 24 and about δOO. The zeohte framework may contain only gallium and silicon atoms or may also contain a combination of gallium, aluminum, and silicon. When the first zeohte is a MFI structure type gallium silicate zeohte, the second zeohte will preferably be an intermediate pore size zeohte having a sihca to gallia mole ratio greater than 100. The second zeohte can also have higher silica to gallia mole ratios, e.g., greater than 200, 500, 1000, etc.

When the first zeohte used in the zeohte bound zeohte catalyst is an aluminosilicate zeohte, the silica to alumina mole ratio will usually depend upon the structure type of the first zeohte and the particular hydrocarbon process in which the catalyst system is utilized and is therefore not hmited to any particular ratio. Generally, however, and depending on the structure type of the zeohte, the first zeohte will have a sihca to alumina mole ratio of at least 2: 1 and in some instances from 4: 1 to about 7: 1. For a number of zeohtes, especially intermediate pore

size zeohtes, the silica to alumina mole ratio will be in the range of from about 10:1 to about 1,000:1. When the catalyst is utilized in acid catalyzed reactions such as cracking, the manufacture of paraxylene and benzene by the disproportionation of toluene, the alkylation of benzene or the like, the zeohte will be acidic and will preferably, when it is an intermediate pore size zeohte, have higher silica to alumina mole ratios, e.g., 20:1 to about 200: 1. If the catalyst system is utilized in a process where acid catalyzed reactions may not desired, such as a the reforming of naphtha, the second zeohte will preferably exhibit reduced acid activity.

The structure type of the first zeolite will depend on the particular hydrocarbon process in which the zeohte catalyst system is utilized. For instance, if the catalyst system is used for the reforming of naphtha to aromatics, the zeohte type will preferably be LTL (example Zeohte L) and have a silica to alumina ratio from 4: 1 to about 7: 1. If the catalyst system is be used for xylene isomerization or the manufacture of paraxylene and benzene by the disproportionation of toluene, the first zeohte will preferably be an intermediate pore size zeolite, such as a MFI structure type (example ZSM-5). If the zeohte catalyst system is to be used for cracking paraffins, the preferred pore size and structure type will depend on the size of the molecules to be cracked and the desired product. The selection of the structure type for hydrocarbon conversion processes is known to persons skilled in the art.

The term "average particle size" as used herein, means the arithmetic average of the diameter distribution of the crystals on a volume basis.

The average particle size of the crystals of the first zeohte is preferably from about 0.1 to about 15 microns. In some apphcations, the average particle size will preferably be at least about 1 to about 6 microns. In other apphcations such as the cracking of hydrocarbons, the preferred average particle size will be from about 0.1 to about 3.0 microns.

The second zeohte will have a structure type that is different from the first zeohte. The structure type of the second zeohte will depend on the intended use of the zeohte bound zeohte catalyst. For instance, if the zeohte bound zeohte catalyst is utilized as an isomerization/ethylbenzene dealkylation catalyst, the first zeohte is preferably selected such that the dealkylation of the ethylbenzene will occur at the catalytic phase of the first zeohte, and xylene isomerization would primarily occur at the catalytic phase of the second zeohte. If the catalyst is to be utilized in a cracking process, the second zeohte will preferably have acid activity and the structure type can be selected such that its pore size allows into its channels the larger molecules where they are subject to cracking into small products. After the larger molecules are cracked by the second zeolite, the cracked molecules can then enter the smaller pores of a first zeohte where they can be subject to further cracking, isomerization, or oligimerization depending on the desired resulting product. Alternatively, the pore size of the second zeohte can be smaller than the pore size of the first zeohte. In this embodiment, the large molecules enter the pores of the first zeohte where they are subject to cracking and then the cracked molecules enter the pores of the second zeohte where they can be subject to further conversion. The catalyst can also be tailored so that the second zeohte crystals sieve feed components entering the pores of the first zeohte or sieve product components exiting the channels of the first zeohte. For instance, if

the zeohte bound zeohte catalyst of the present invention comprises an appropriate pore size second zeohte, it can function to sieve and sort out molecules based on their size or shape and thereby prevent undesirable molecules from entering or exiting, as the case may be, the catalytic phase of the first zeohte.

When the second zeohte is aluminosilicate zeohte, the sihca to alumina mole ratio of the second zeolite, will usually depend upon the structure type of the second zeolite and particular hydrocarbon process in which the catalyst is utilized and is therefore not hmited to any particular ratio. Generally, however, and depending on the structure type of the zeohte, the silica to alumina ratio will be at least 2: 1. In apphcations where the aluminosilicate zeohte is an intermediate pore size zeohte and low acidity is desired, the second zeohte preferably has a sihca to alumina mole ratio greater than the silica to alumina mole ratio of the first zeohte, and more preferably is greater than 200: 1. The second zeohte can also have higher silica to alumina mole ratios, e.g., 300:1, 500: 1, 1,000: 1, etc. In certain apphcations, the second zeohte can be a Sihcalite i.e., the second zeohte is a MFI structure type substantially free of alumina or Sihcalite 2, i.e., the second zeohte is a MEL structure type substantially free of alumina. The pore size of the second zeohte will preferably be a pore size that does not adversely restrict access of the desired molecules of the hydrocarbon feedstream to the catalytic phase of the first zeohte. For instance, when the materials of the feedstream which are to be converted by the first zeohte have a size from 5 A to 6.8 A, the second zeohte will preferably be a large pore zeohte or an intermediate pore size zeohte.

The second zeohte is usually present in the zeohte bound zeohte catalyst in an amount in the range of from about 10 to about 60 % by

weight based on the weight of the first zeohte but the amount of second zeohte present will usually depend on the hydrocarbon process in which the catalyst is utilized. More preferably the amount of second zeohte present is from about 20 to about 50% by weight.

The second zeohte crystals preferably have a smaller size than the first zeohte crystals. The second zeohte crystals preferably have an average particle size of less than 1 micron, preferably from about 0.1 to less than 0.5 micron. The second zeohte crystals, in addition to binding the first zeohte particles and maximizing the performance of the catalyst will preferably intergrow and to form an over-growth which coats or partially coats the first zeohte. Preferably, the coating will be resistant to attrition.

The zeohte bound zeohte catalyst is preferably prepared by a three step procedure. The first step involves the synthesis of the first zeohte core crystals. Processes for preparing the first zeohte are known to persons skilled in the art. For example, with respect to the preparation of a MFI structure type, such as ZSM-5, a preferred process comprises preparing a solution containing tetrapropyl ammonium hydroxide or bromide, alkali metal oxide, an oxide of aluminum, an oxide of silicon and water, heating the reaction mixture to a temperature of 80°C to 200°C for a period of from about four hours to eight days. The resulting gel forms sohd crystal particles which are separated from the reaction medium, washed with water and dried. The resulting product can be calcined in air at temperatures of 400- 550°C for a period of 10-40 hours to remove tetrapropylammonium (TPA) cations.

Next, a silica-bound zeolite is prepared preferably by mixing a mixture comprising the zeohte crystals, a silica gel or sol, water and optionally an extrusion aid until a homogeneous composition in the form of an extrudable paste develops. The sihca binder used in preparing the sihca bound zeohte aggregate is preferably a silica sol and can contain various amounts of trivalent metal oxides such as alumina. The amount of zeohte in the dried extrudate at this stage will preferably range from about 40 to 90% by weight, more preferably from about 50 to 80% by weight, with the balance being primarily silica, e.g. about 20 to 50% by weight silica.

The resulting paste is then molded, e.g. extruded, and cut into small strands, e.g., 2 mm diameter extrudates, which are dried at 100-150°C for a period of 4-12 hours and then calcined in air at a temperature of from about 400°C to 550°C for a period of from about 1 to 10 hours.

Optionally, the silica-bound aggregate can be made into a very small particles which have application in fluid bed processes such as catalytic cracking. This preferably involves mixing the zeohte with a silica containing matrix solution so that an aqueous solution of zeohte and silica binder is formed which can be sprayed dried to result in small fluidizable silica-bound aggregate particles. Procedures for preparing such aggregate particles are known to persons skilled in the art. An example of such a procedure is described by Scherzer (Octane- Enhancing Zeohtic FCC Catalysts, Juhus Scherzer, Marcel Dekker, Inc. New York, 1990). The fluidizable silica-bound aggregate particles, hke the sihca bound extrudates described above, would then undergo the final step described below to convert the silica binder to a second zeohte.

The final step in the three step catalyst preparation process is the conversion of the silica present in the silica-bound zeohte to a second zeohte having a structure type different from the first zeohte. The crystals of the second zeohte bind the first zeohte crystals together. The first zeohte crystals are thus held together without the use of a significant amount of non-zeohte binder.

To prepare the zeohte bound zeohte, the silica-bound aggregate is preferably first aged in an appropriate aqueous solution at elevated temperature. Next, the contents of the solution and the temperature at which the aggregate is aged are selected to convert the amorphous silica binder into the desired second zeohte. The newly-formed second zeohte is produced as crystals. The crystals may grow on and/or adhere to the first zeohte crystals, and may also be produced in the form of new intergrown crystals, which are generally much smaller than the initial crystals, e.g., of sub -micron size. These newly formed crystals may grow together and interconnect.

The nature of the zeohte formed in the secondary synthesis conversion of the silica to zeohte may vary as a function of the composition of the secondary synthesis solution and synthesis aging conditions. The secondary synthesis solution is preferably an aqueous ionic solution containing a source of hydroxy ions sufficient to convert the silica to the desired zeohte. It is important, however, that the aging solution be of a composition which will not cause the sihca present in the bound zeohte extrudate to dissolve out of the extrudate.

The first and second zeohtes may be further ion exchanged as is known in the art either to replace at least in part the original metals present in the zeohte with a different cation, e.g. a Group IB to VIII of the

Periodic Table metal such as nickel, copper, zinc, calcium or rare earth metal, or to provide a more acidic form of the zeohte by exchange of alkali metal with intermediate ammonium, followed by calcination of the ammonium form to provide the acidic hydrogen form. The acidic form may be readily prepared by ion exchange using a suitable acidic reagent such as ammonium nitrate. The zeohte catalyst may then be calcined at a temperature of 400-550°C for a period of 10-45 hours to remove ammonia and form the acidic hydrogen form. Ion exchange is preferably conducted after formation of the zeohte bound zeohte catalyst. Particularly preferred cations are those which render the material catalytically active, especially for certain hydrocarbon conversion reactions. These include hydrogen, rare earth metals, and metals of Groups IIA, IIIA, IVA, IB, LIB, IIIB, IVB, and VIII of the Periodic Table of the Elements. For some hydrocarbon conversion processes, the zeohte bound zeohte catalyst will contain a catalytically active metal such as at least one Group VIII metal, such as for example, platinum, palladium, rhodium, osmium, iridium, and ruthenium.

The zeohte catalyst systems of the present invention can be used in processing hydrocarbon feedstocks. Hydrocarbon feed-stocks contain carbon compounds and can be from many different sources, such as virgin petroleum fractions, recycle petroleum fractions, tar sand oil, and, in general, can be any carbon containing fluid susceptible to zeohtic catalytic reactions. Depending on the type of processing the hydrocarbon feed is to undergo, the feed can contain metal or can be free of metals. Also, the feed can also have high or low nitrogen or sulfur impurities.

The conversion of hydrocarbon feeds can take place in any convenient mode, for example, in fluidized bed, moving bed, or fixed bed reactors depending on the types of process desired.

Since the zeohte bound zeohte catalyst of the present invention has controlled acidity, does not contain a conventional binder which can adversely affect the access and/or contact of reactants to and with the active sites of the catalyst and can also cause undesirable side reactions to occur, and if desired, can be tailored to maximize its performance, the zeohte bound zeohte catalyst of the present invention by itself or in combination with one or more catalytically active substances can be used as a catalyst or support for a variety of organic, e.g., hydrocarbon compound, conversion processes. Examples of such conversion processes include, as non-hmiting examples, the following:

(A) The catalytic cracking of a naphtha feed to produce hght olefins. Typical reaction conditions include from about 500°C to about 750°C, pressures of subatmospheric or atmospheric, generally ranging up to about 10 atmospheres (gauge) and residence time (volume of the catalyst „ feed rate) from about 10 milliseconds to about 10 seconds.

(B) The catalytic cracking of high molecular weight hydrocarbons to lower weight hydrocarbons. Typical reaction conditions for catalytic cracking include temperatures of from about 400°C to about 700°C, pressures of from about 0.1 atmosphere (bar) to about 30 atmospheres, and weight hourly space velocities of from about 0.1 to about lOOhr ¹ .

(C) The transalkylation of aromatic hydrocarbons in the presence of polyalkylaromatic hydrocarbons. Typical reaction conditions include a temperature of from about 200°C to about 500°C, a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about 1 to about lOOhr - ¹ and an aromatic hydrocarbon/polyalkylaromatic hydrocarbon mole ratio of from about 1/1 to about 16/1.

(D) The isomerization of aromatic (e.g., xylene) feedstock components. Typical reaction conditions for such include a temperature of from about 230°C to about 510°C, a pressure of from about 0.5 atmospheres to about 50 atmospheres, a weight hourly space velocity of from about

0.1 to about 200 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 100.

(E) The dewaxing of hydrocarbons by selectively removing straight chain paraffins. The reaction conditions are dependent in large measure on the feed used and upon the desired pour point. Typical reaction conditions include a temperature between about 200°C and 450°C, a pressure up to 3,000 psig and a hquid hourly space velocity from 0.1 to 20.

(F) The alkylation of aromatic hydrocarbons, e.g., benzene and alkylbenzenes, in the presence of an alkylating agent, e.g., olefins, formaldehyde, alkyl halides and alcohols having 1 to about 20 carbon atoms. Typical reaction

conditions include a temperature of from about 100°C to about 500°C, a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about lhr - ¹ to about lOOhr ^! and an aromatic hydrocarbon/alkylating agent mole ratio of from about 1/1 to about 20/1.

(G) The alkylation of aromatic hydrocarbons, e.g., benzene, with long chain olefins, e.g., C14 olefin. Typical reaction conditions include a temperature of from about 50°C to about 200°C, a pressure of from about atmospheric to about 200 atmospheres, a weight hourly space velocity of from about 2 hr"* to about 2000 hr'l and an aromatic hydrocarbon/olefin mole ratio of from about 1/1 to about 20/1. The resulting product from the reaction are long chain alkyl aromatics which when subsequently sulfonated have particular apphcation as synthetic detergents;

(H) The alkylation of aromatic hydrocarbons with hght olefins to provide short chain alkyl aromatic compounds, e.g., the alkylation of benzene with propylene to provide cumene. Typical reaction conditions include a temperature of from about 10°C to about 200°C, a pressure of from about 1 to about 30 atmospheres, and an aromatic hydrocarbon weight hourly space velocity (WHSV) of from 1 hr ^~ l to about 50 hr'l;

(I) The hydrocracking of heavy petroleum feedstocks, cyclic stocks, and other hydrocrack charge stocks. The zeohte

catalyst system will contain an effective amount of at least one hydrogenation component of the type employed in hydrocracking catalysts.

(J) The alkylation of a reformate containing substantial quantities of benzene and toluene with fuel gas containing short chain olefins (e.g., ethylene and propylene) to produce mono- and dialkylates. Preferred reaction conditions include temperatures from about 100°C to about 250°C, a pressure of from about 100 to about 800 psig, a WHSV -olefin from about 0.4 hr ¹ to about 0.8 hr'l, a WHSV -reformate of from about 1 hr'l to about 2 hr"l and, optionally, a gas recycle from about 1.5 to 2.5 vol/vol fuel gas feed.

(K) The alkylation of aromatic hydrocarbons, e.g., benzene, toluene, xylene, and naphthalene, with long chain olefins, e.g., C14 olefin, to produce alkylated aromatic lube base stocks. Typical reaction conditions include temperatures from about 100°C to about 400°C and pressures from about 50 to 450 psig.

(L) The alkylation of phenols with olefins or equivalent alcohols to provide long chain alkyl phenols. Typical reaction conditions include temperatures from about

100°C to about 250°C, pressures from about 1 to 300 psig and total WHSV of from about 2 hr" ¹ to about 10 hr ^{" 1} .

(M) The conversion of hght paraffins to olefins and/or aromatics. Typical reaction conditions include

temperatures from about 425°C to about 760°C and pressures from about 10 to about 2000 psig.

(N) The conversion of hght olefins to gasohne, distillate and lube range hydrocarbons. Typical reaction conditions include temperatures of from about 175°C to about 375°C and a pressure of from about 100 to about 2000 psig.

(O) Two-stage hydrocracking for upgrading hydrocarbon streams having initial boiling points above about 200°C to premium distillate and gasohne boiling range products or as feed to further fuels or chemicals processing steps. The first stage would be the zeohte catalyst system comprising one or more catalytically active substances, e.g., a Group VIII metal, and the effluent from the first stage would be reacted in a second stage using a second zeohte, e.g., zeohte Beta, comprising one or more catalytically active substances, e.g., a Group VIII metal, as the catalyst. Typical reaction conditions include temperatures from about 315°C to about 455°C, a pressure from about 400 to about 2500 psig, hydrogen circulation of from about 1000 to about 10,000 SCF/bbl and a hquid hourly space velocity (LHSV) of from about 0.1 to 10;

(P) A combination hydrocracking/de waxing process in the presence of the zeohte bound zeohte catalyst comprising a hydrogenation component and a zeohte such as zeohte Beta. Typical reaction conditions include temperatures from about 350°C to about 400°C, pressures from about

1400 to about 1500 psig, LHSVs from about 0.4 to about 0.6 and a hydrogen circulation from about 3000 to about 5000 SCF/bbl.

(Q) The reaction of alcohols with olefins to provide mixed ethers, e.g., the reaction of methanol with isobutene and/or isopentene to provide methyl-t-butyl ether (MTBE) and/or t-amyl methyl ether (TAME). Typical conversion conditions include temperatures from about 20°C to about 200°C, pressures from 2 to about 200 atm, WHSV (gram- olefin per hour gram-zeolite) from about 0.1 hr"l to about 200 hr ^{- 1} and an alcohol to olefin molar feed ratio from about 0.1/1 to about 5/1.

(R) The disproportionation of aromatics, e.g. the disproportionation toluene to make benzene and paraxylene. Typical reaction conditions include a temperature of from about 200°C to about 760°C, a pressure of from about atmospheric to about 60 atmosphere (bar), and a WHSV of from about 0.1 hr" ¹ to about 30 hr ¹ .

(S) The conversion of naphtha (e.g. Ce - Cio) and similar mixtures to highly aromatic mixtures. Thus, normal and shghtly branched chained hydrocarbons, preferably having a boiling range above about 40°C, and less than about 200°C, can be converted to products having a substantial higher octane aromatics content by contacting the hydrocarbon feed with the zeohte at a temperature in the range of from about 400°C to 600°C, preferably 480°C

to 550 ^C C at pressures ranging from atmospheric to 40 bar, and hquid hourly space velocities (LHSV) ranging from 0.1 to 15.

(T) The adsorption of alkyl aromatic compounds for the purpose of separating various isomers of the compounds.

(U) The conversion of oxygenates, e.g., alcohols, such as methanol, or ethers, such as dimethylether, or mixtures thereof to hydrocarbons including olefins and aromatics with reaction conditions including a temperature of from about 275°C to about 600°C, a pressure of from about 0.5 atmosphere to about 50 atmospheres and a hquid hourly space velocity of from about 0.1 to about 100.

(V) The ohgomerization of straight and branched chain olefins having from about 2 to about 5 carbon atoms. The ohgomers which are the products of the process are medium to heavy olefins which are useful for both fuels, i.e., gasohne or a gasohne blending stock, and chemicals.

The ohgomerization process is generally carried out by contacting the olefin feedstock in a gaseous state phase with a zeohte bound zeohte at a temperature in the range of from about 250°C to about 800°C, a LHSV of from about 0.2 to about 50 and a hydrocarbon partial pressure of from about 0.1 to about 50 atmospheres. Temperatures below about 250°C may be used to ohgomerize the feedstock when the feedstock is in the hquid phase when contacting the zeohte bound zeohte catalyst. Thus, when the olefin feedstock contacts the catalyst in the liquid phase,

temperatures of from about 10°C to about 250°C may be used.

(W) The conversion of C2 unsaturated hydrocarbons (ethylene and/or acetylene) to aliphatic Cβ-ia aldehydes and converting said aldehydes to the corresponding Co 12 alcohols, acids, or esters.

In general, the, catalytic conversion conditions over the zeohte bound zeohte catalyst include a temperature of from about 100°C to about 760°C, a pressure of from about 0.1 atmosphere (bar) to about 200 atmospheres (bar), a weight hourly space velocity of from about 0.08 hr - ¹ to about 2,000 hr ¹ .

Although many hydrocarbon conversion processes prefer that the second zeohte crystals have lower acidity to reduce undesirable reactions external to the first zeohte crystals, some processes prefer that the second zeohte crystals have higher acidity, e.g., cracking reactions.

Processes that find particular apphcation using the zeohte bound zeohte catalyst of the present invention are those where two or more reactions are taking place within the zeohte bound zeohte catalyst. This catalyst would comprise two different zeohtes that are each separately tailored to promote or inhibit different reactions. A process using such a catalyst benefits not only from greater apparent catalyst activity, greater zeohte accessibility, and reduced non-selective surface acidity possible with zeohte bound zeohtes, but from a tailored catalyst system.

Examples of zeohte bound zeohte catalysts and exemplary uses are shown below in Table I:

Table I

Examples of preferred zeohte bound zeohte catalyst systems include the following:

1. A zeohte bound zeohte catalyst system comprising an acidic second zeohte having cracking activity and an acidic first zeohte having acidic activity which is less than the acidic activity of the second zeohte and a smaller pore size than the second zeohte. The zeohte bound zeohte catalyst system finds particular apphcation in cracking larger size molecules and isomerizing the smaller cracked molecules. Examples of suitable second zeohtes include Beta, Mordenite and the like. Examples of suitable first zeohtes are ZSM-5, ZK-5, ZSM-11 and the hke.

2. A zeohte bound zeohte catalyst system comprising an acidic first zeohte having a large or medium pore zeohte with cracking activity and an acidic second zeohte having smaller pore size than the second zeohte and having cracking activity. An example of a suitable first zeohte ZSM-5 and an example of a suitable second zeohte is ZK- 5. The zeohte bound zeohte catalyst system finds particular apphcation in cracking larger size molecules and further cracking the smaller cracked molecules to produce ethylene.

3. A zeohte catalyst system comprising one zeohte (either the first or second zeohte) that has reduced acid activity and optionally contains a hydrogenation/dehydrogenation metal and another zeohte which has medium strength acidic activity and optionally a hydrogenation/ dehydrogenation metal. The pore size of the zeohtes will depend upon the type of process in which the catalyst

system is utilized. For example, the catalyst system can be utilized in a combined xylene isomerization/ ethylbenzene dealkylation process wherein the ethylbenzene is dealkylated to benzene and ethane and isomers of xylenes are isomerized to equilibrium amounts.

In such a system, the first zeohte will preferably have a large or intermediate pore size zeohte and the second zeohte will also preferably have a larger or intermediate pore size zeolite.

4. A zeohte bound zeohte catalyst comprising a first acidic zeohte and a second zeohte which has httle or no acidic activity. The pore size of the zeohtes will depend on the type of process in which the catalyst is utilized. For example, if the catalyst is to be used in the manufacture of benzene and paraxylene by the disproportionation of toluene, the first zeohte will preferably have an intermediate pore size and the second zeohte can be selected to enhance performance of the first zeohte, e.g., to sieve undesired molecules either leaving the first zeohte phase or exiting the first zeohte phase, as the case may be or to control accessibility of the acid sites on the external surfaces of its first zeohte to reactants. Catalysts A and D in Table I are examples of such a catalyst.

The zeohte-bound zeohte catalyst of the present invention has particular apphcation in the vapor phase disproportionation of toluene. Such vapor phase disproportionation comprises contacting toluene under disproportionation conditions with the zeohte bound zeohte catalyst to yield a product mixture which comprises a mixture of

unreacted (unconverted) toluene, benzene and xylene. In the more preferred embodiment, the catalyst is first selectivated prior to use in the disproportionation process to enhance conversion of toluene to xylene and to maximize the catalyst selectivity towards the production of paraxylene. Processes for selectivating the catalyst are known to persons skilled in the art. For instance, selectivation may be accomplished by exposing the catalyst in a reactor bed to a thermally decomposable organic compound, e.g. toluene, at a temperature in excess of the decomposition temperature of said compound, e.g. from about 480°C to about 650°C, more preferably 540°C to about 650°C, at a WHSV in the range of from about 0.1 to 20 lbs of feed per pound of catalyst per hour, at a pressure in the range of from about 1 to 100 atmospheres, and in the presence of 0 to about 2 moles of hydrogen, more preferably from about 0.1 to about 2 moles of hydrogen per mole of organic compound, and optionally in the presence of 0-10 moles of nitrogen or another inert gas per mole of organic compound. This process is conducted for a period of time until a sufficient quantity of coke has been deposited on the catalyst surface, generally at least about 2% by weight and more preferably from about 8 to about 40% by weight of coke. In a preferred embodiment, such a selectivation process is conducted in the presence of hydrogen in order to prevent rampant formation of coke on the catalyst.

Selectivation of the catalyst can also be accomphshed by treating the catalyst with a selectivation agent such as an organosilicon compound. Examples of organosilicon compounds include polysiloxane including silicones, a siloxane, and a silane including disilanes and alkoxysilanes.

Sihcone compounds that find particular apphcation can be represented by the formula:

wherein Ri is hydrogen, fluoride, hydroxy, alkyl, aralkyl, alkaryl or fluoro-alkyl. The hydrocarbon substituents generally contain from 1 to 10 carbon atoms and preferably are methyl or ethyl groups. R2 is selected from the same group as Ri, and n is an integer of at least 2 and generally in the range of 2 to 1000. The molecular weight of the sihcone compound employed is generally between 80 and 20,000 and preferably 150 to 10,000. Representative sihcone compounds included dimethylsihcone, diethylsilicone, phenylmethylsihcone, methyl hydrogensilicone, ethylhydrogensilicone, phenylhydrogensilicone, methylethylsilicone, phenylethylsilicone, diphenylsilicone, methyltri fluoropropylsilicone, ethyltrifluoropropylsilicone, tetrachlorophenyl methyl sihcone, tetrachlorophenylethyl sihcone, tetrachloro phenylhydrogen sihcone, tetrachlorophenylphenyl sihcone, m ethyl vinylsihcone and ethylvinylsilicone. The sihcone compound need not be hnear but may be cychc as for example hexamethylcyclotrisiloxane, octamethylcyclotetrasiloxane, hexaphenyl cyclotrisiloxane and octaphenylcyclotetrasiloxane. Mixtures of these compounds may also be used as well as silicones with other functional groups.

Useful siloxanes or polysiloxanes include as non-hmiting examples hexamethylcyclotrisiloxane, octamethylcyclotetrasiloxane, decamethyl

cyclopentasiloxane, hexamethyldisiloxane, octamethytrisiloxane, decamethyltetrasiloxane, hexaethylcyclotrisiloxane, octaethylcyclo tetrasiloxane, hexaphenylcyclotrisiloxane and octaphenylcyclo tetrasiloxane.

Useful silanes, disilanes, or alkoxysilanes include organic substituted silanes having the general formula:

Si

R,

wherein R is a reactive group such as hydrogen, alkoxy, halogen, carboxy, amino, acetamide, trialkylsilyoxy Ri, R2 and R3 can be the same as R or can be an organic radical which may include alkyl of from 1 to 40 carbon atoms, alkyl or aryl carboxyhc acid wherein the organic portion of the alkyl contains 1 to 30 carbon atoms and the aryl group contains 6 to 24 carbon which may be further substituted, alkylaryl and arylalkyl groups containing 7 to 30 carbon atoms. Preferably, the alkyl group for an alkyl silane is between 1 and 4 carbon atoms in chain length.

When used the vapor phase disproportionation of toluene, the catalyst can comprise a first phase of particles of MFI-type zeohte crystals having a micron average particle size from about 2 to about 6, a silica to alumina mole ratio of from about 20 to about 200: 1, preferably, 25: 1 to about 120: 1, having adhered structurally to the surfaces thereof particles of a second MEL-type zeohte binder phase having an average

particle size of less than about 0.1 micron and having a alumina to silica mole ratio in excess of about 200: 1 to about 10,000:1 and most preferably greater than 500: 1 including Silicahte 2.

Once the catalyst has been selectivated to the desired degree, reactor selectivation conditions are changed to disproportionation conditions. Disproportionation conditions include a temperature between about 400°C and 550°C, more preferably between about 425°C and 510°C, at a hydrogen to toluene mole ratio of from 0 to about 10, preferably between about 0.1 and 5 and more preferably from about 0.1 to 1, at a pressure between about 1 atmosphere and 100 atmospheres and utilizing WHSV of between about 0.5 and 50

The disproportionation process may be conducted as a batch, semi- continuous or continuous operation using a fixed or moving bed catalyst system deposited in a reactor bed. The catalyst may be regenerated after coke deactivation by burning off the coke to a desired extent in an oxygen-containing atmosphere at elevated temperatures as know in the art.

The zeohte bound zeohte of the present invention also finds particular apphcation as a catalyst in a process for isomerizing one or more xylene isomers in a Cβ aromatic feed to obtain ortho-, meta-, and para¬ xylene in a ratio approaching the equilibrium value. In particular, xylene isomerization is used in conjunction with a separation process to manufacture para-xylene. For example, a portion of the para-xylene in a mixed Cs aromatics stream may be recovered using processes known in the art, e.g., crystallization, adsorption, etc. The resulting stream is then reacted under xylene isomerization conditions to restore ortho-, meta-, and paraxylenes to a near equilibrium ratio.

Ethylbenzene in the feed is either removed from the stream or is converted during the process to xylenes or to benzene which are easily separated by distillation. The isomerate is blended with fresh feed and the combined stream is distilled to remove heavy and hght by- products. The resultant Cs aromatics stream is then recycled to repeat the cycle.

It is important that xylene isomerization catalysts produce a near equilibrium mixture of xylenes and it is also usually desirable that the catalyst convert ethylbenzene with very httle net loss of xylenes. The zeohte bound zeohte catalyst finds particular apphcation in this regard. The silica to alumina mole ratios of the first zeohte and second zeolite can be selected to balance xylene isomerization and ethylbenzene dealkylation while minimizing undesirable side reactions. Accordingly, the zeohte catalyst of the present invention finds particular application in a hydrocarbon conversion process which comprises contacting a Cβ aromatic stream containing one or more xylene isomers or ethylbenzene or a mixture thereof, under isomerization conditions with the zeohte bound zeohte catalyst. Preferably, at least 30% of the ethylbenzene is converted.

In the vapor phase, suitable isomerization conditions include a temperature in the range 250°C - 600°C, preferably 300°C - 550°C, a pressure in the range 0.5 - 50 atm abs, preferably 10 - 25 atm abs, and a weight hourly space velocity (WHSV) of 0.1 to 100, preferably 0.5 to

50. Optionally, isomerization in the vapor phase is conducted in the presence of 3.0 to 30.0 moles of hydrogen per mole of alkylbenzene. If hydrogen is used, the metal components of the catalyst preferably include 0.1 to 2.0 wt.% of a hydrogenation/dehydrogenation component selected from Group VIII of the Periodic Table of Elements, especially

platinum, palladium, or nickel. By Group VIII metal component, it is meant the metals and their compounds such as oxides and sulfides.

In the liquid phase, suitable isomerization conditions include a temperature in the range 150°C - 375°C, a pressure in the range 1 - 200 atm abs, and a WHSV in the range 0.5 - 50. Optionally, the isomerization feed may contain 10 to 90 wt.% of a diluent such as toluene, trimethylbenzenes, naphthenes, or paraffins.

The zeohte bound zeohte catalyst of the present invention are especially useful as a catalyst in a process for cracking a naphtha feed, e.g., CΛ ⁺ naphtha feed, particularly a Cr 290°C naphtha feed to produce low molecular weight olefins, e.g., C2 through C4 olefins, particularly ethylene and propylene. Such a process is preferably carried out by contacting the naphtha feed at temperatures ranging from 500°C to about 750°C, more preferably 550°C to 675°C, at a pressure from sub atmospheric up to 10 atmospheres, but preferably from about 1 atmosphere to about 3 atmospheres.

The zeohte bound zeohte catalyst of the present invention is especially useful as a catalyst in the transalkylation of polyalkylaromatic hydrocarbons. Examples of suitable polyalkylaromatic hydrocarbons include di-, tri-, and tetra-alkyl aromatic hydrocarbons, such as diethylbenzene, triethylbenzene, diethylmethylbenzene (diethyl- toluene), diisopropyl-benzene, triisopropylbenzene, diisopropyltoluene, dibutylbenzene, and the hke. Preferred polyalkylaromatic hydro¬ carbons are the dialkyl benzenes. Particularly preferred polyalkyl¬ aromatic hydrocarbons are diisopropylbenzene and diethylbenzene.

The transalkylation process will preferably have a molar ratio of aromatic hydrocarbon to polyalkylaromatic hydrocarbon of preferably from about 0.5: 1 to about 50: 1, and more preferably from about 2: 1 to about 20: 1. The reaction temperature will preferably range from about 340°C to 500°C to maintain at least a partial hquid phase, and the pressure will be preferably in the range of about 50 psig to 1,000 psig, preferably 300 psig to 600 psig. The weight hourly space velocity will range from about 0.1 to 10.

The zeohte bound zeohte catalyst is also useful in processes for converting aromatic compounds from paraffins. Example of suitable paraffins including aliphatic hydrocarbons containing 2 to 12 carbon atoms. The hydrocarbons may be straight chain, open or cychc and may be saturated or unsaturated. Example of hydrocarbons include propane, propylene, n-butane, n-butenes, isobutane, isobutene, and straight- and branch-chain and cychc pentanes, pentenes, hexanes, and hexenes.

The aromatization conditions include a temperature of from about 200°C to about 700°C, a pressure of from about 0.1 atmosphere to about 60 atmospheres, a weight hourly space velocity (WHSV) of from about 0.1 to about 400 and a hydrogen/hydrocarbon mole ratio of from about 0 to about 20.

The zeohte bound zeohte catalyst used in the aromatization process preferably comprises first crystals of an intermediate pore size zeohte such a MFI type zeohte (example ZSM-5), and second crystals of a intermediate pore size such as a MEL structure type. The catalyst preferably contains gallium. Gallium may be incorporated into the during synthesis of the zeohte or it may be exchanged or impregnated

or otherwise incorporated into the zeohte after synthesis. Preferably 0.05 to 10, and most preferably 0.1 to 2.0 wt.% gallium is associated with the zeohte bound zeolite catalyst. The gallium can be associated with the first zeohte, second zeohte, or both zeohtes.

The following examples illustrate the invention.

EXAMPLE 1

Preparation of Zeohte KL Bound by Offeretite

Zeohte KL crystals were prepared from a synthesis gel having the following composition expressed in moles of pure oxide:

2.7 K2θ/1.0 Al ₂ θ3/9.2 Siθ2: 150 H ₂ O

The gel was prepared as follows:

Aluminum hydroxide was dissolved in a aqueous solution of potassium hydroxide (50% pure KOH) to form Solution A. After dissolution, water loss was corrected. A separate solution, Solution B, was prepared by diluting colloidal silica (LUDOX HS 40) with water.

Solutions A and B were mixed and preheated to 150°C and held at that temperature for 90 hours to bring about crystalhzation. After crystalhzation, the crystals were washed and calcined.

The formed zeohte KL was highly crystalline and the crystals were cylindrical and had a length from 0.5 to 1.5 microns and a diameter from 0.5 to 2.0 microns.

The zeohte KL was formed into sihca bound extrudates as follows:

The above components were mixed in a household mixed in the order shown. After adding the methocel, a thickened and extrudable dough was obtained. The total mixing time was about 28 minutes.

The dough was extruded into 2 mm extrudates, dried overnight at 100°C, broken into 0.5- lmm pieces and then calcined at 505°C for 6 hours in air.

Composition of silica-bound extrudates:

Zeohte KL: 70 wt.% Si0 ₂ Binder: 30 wt.%

The silica-bound zeohte KL extrudates were converted into zeohte KL bound by offretite as follows:

Solution A was prepared by dissolving the ingredients into boiling water and coohng the solution to ambient temperature. Water loss due to boiling was corrected.

Solution A was poured into a 300 ml stainless steel autoclave. Solution B was poured into the contents of the autoclave. The two solutions were mixed by swirling the autoclave. Finally, 50.02 grams of the silica-bound zeohte KL extrudates were added into the contents of the autoclave. The molar composition of synthesis mixture was:

2.20 K2O/1.50 TMAC1/1.26 AI2O3/IO SiO ₂ /160 H2O

In the mixture, the silica is present as the binder in the extrudate.

The autoclave was heated up to 150°C in 2 hours and kept at this temperature for 72 hours. After the aging period, the autoclave was opened and the product-extrudates were collected.

The product was washed in a Buechner funnel to a pH of 9.6. The product was dried overnight at 150°C and subsequently calcined in air for 16 hours at 500°C. The amount of product was 55.6 grams and consisted of zeohte KL crystals which were bound by an overgrowth of offretite crystals The product had excellent strength.

The product extrudates were characterized by x-ray diffraction (XRD), scanning electron microscopy (SEM) and hexane adsorption, with the following results:

XRD: Showed the presence of zeohte L and offretite. The product had excellent crystallinity and no amorphous silica was present.

SEM: Micrographs showed that the Zeohte KL crystals are overgrown with newly formed offretite crystals.

Hexane Adsorption: 7.8 wt.%

EXAMPLE 2

Preparation of Zeohte Y Bound by EMT Structure Type Zeohte

Zeohte Y crystals were formed into silica bound Zeohte Y as follows:

Components 1 and 3 were mixed in the bowl of a household mixer. Next, components 2 and 4 were added to the bowl and the contents were mixed. Component 5 was then added to the bowl and the mixing continued. Total mixing time was about 28 minutes. A plastic extrudable dough was obtained. The dough was extruded into 2 mm extrudates. The extrudates were dried overnight at 150°C and then

calcined for 7.5 hours at 525°C. The extrudates contained 30.09 weight percent sihca.

The sihca bound zeohte Y extrudates were converted into Zeohte Y bound by EMT structure type zeohte as follows:

Components 1 and 2 were dissolved into component 3 by boiling to form a solution. In a 100 ml. plastic bottle, component 5 was dissolved into component 6. Component 7 was added to the contents of the plastic bottle. The solution was added together with component 4 into the plastic bottle. The bottle was mixed to ensure a homogeneous mixture. Finally component 8 was then added to the bottle. The molar composition of the synthesis mixture was:

2.32 Na ₂ O/0.77 C.E. 18-6/Al ₂ O ₃ /10 SiO ₂ /183 H ₂ O

The plastic bottle was placed into a 98°C oil bath. After 15 days of heating at that temperature, crystalhzation was stopped. The product extrudates were washed 5 times with 800 ml water at 60°C. The conductivity of the last wash water was 70 μS/cm. The product was dried overnight at 120°C. Next, the extrudates were calcined at 500°C

for 9 hrs. The amount of product recovered after calcination was 31.70

The product extrudates were characterized by x-ray diffraction (XRD), scanning electron microscopy (SEM) and hexane adsorption with the following results:

XRD: Showed excellent crystalhnity and the presence of EMT structure type. No amorphous halo could be seen, which would have indicated the presence of unconverted silica. Zeohte P was completely absent.

SEM: 10,000 times Micrographs (FIG. 1) show that the zeohte Y crystals are coated and glued with platelet hke crystallites with newly formed EMT structure type zeohte.

Hexane adsorption: 14.7 wt.%

EXAMPLE 3

Preparation of MFI Bound by MEL

A MFI structure type zeolite having a silica to alumina mole ration of about 78 and bound by about 30% by weight silica was formed into a MFI structure type zeohte bound by Silicate 2 as follows:

Solution A and B were poured into a 200 ml stainless steel autoclave. The contents of the autoclave were mixed. Finally, 75.02 grams of the sihca bound MFI were added to the autoclave. The molar composition of the synthesis mixture was:

0.48Na ₂ 0/0.95 TBA Br/10Si0 ₂ /148H ₂ 0

The autoclave was placed into an oven at ambient temperature. The oven was heated to 150°C and was maintained at 150°C for 80 hours. The resulting product was washed 6 times at 60°C with 2500 ml of water. The conductivity of the last wash water was 80 μS/cm. The product was dried overnight at 120°C and calcined in air at 300°C for 16 hours.

The product was analyzed by XRD and SEM with the following results:

XRD: Showed exceUent crystalhnity and the presence of MEL structure type zeohte.

SEM: 10,000 times Micrographs (FIG 2) show that the MFI crystals are intergrown with smaller crystals.

EXAMPLE 4

The calcined, zeohte bound zeohte catalyst described in Example 3, was selectivated by feeding toluene across the catalyst under the conditions set forth in Table II below:

TABLE II

Selectivation Conditions

Following selectivation, the catalyst was used for the dispropor¬ tionation of toluene under the test conditions shown in Table III below. The catalyst was evaluated under 3 separate test conditions as shown in Table III. On-oil catalyst performance for the catalyst is also shown in Table III.

TABLE πi

On-Oil Conditions

On-Oil Catalyst Performance

The results show the high catalyst activity and PX selectivity of the MEL-bound MFI catalyst.

EXAMPLE 5

I. Catalyst A - ALPO-5 bound SAPO-34

SAPO-34 bound by 30% by weight alumina was formed into AIPO-5 bound SAPO-34 as follows:

Amounts of 4.18 grams of 85% aqueous H3PO4, 10.78 grams of water, and 2.65 grams of tripropylamine (TPA) were added to a 300 ml Teflon fined autoclave in the order hsted. The mixture was stirred to give a homogeneous solution. Next, 10 grams of dried extrudates (1/16" diameter) of the alumina bound SAPO-34 were added to the contents in the autoclave. The extrudates were completely covered by the hquid. The molar composition of the synthesis mixture was:

TPA/AI2O3/P2O5/H2O of 0.63/1.0/0.62/23.4

In the mixture, the alumina accounts for only the alumina binder of the extrudate and the P2O5 accounts for only 85% aqueous H3PO4. The autoclave was sealed and the mixture was heated in 2 hours to 200°C and held without stirring for 24 hours at 200°C. The autoclave was cooled to room temperature and the mother hquor was decanted. The extrudates were washed with de-ionized water until the conductivity of the filtrate was less than 100 micro-Siemens. XRD analysis showed typical patterns for both SAPO-34 and ALPO-5.

II. Catalyst B - ALPO- 11 bound SAPO-34

SAPO-34 bound by 25% by weight alumina was formed into ALPO- 11 bound SAPO-34 as follows:

Amounts of 6.36 grams of 85% aqueous H3PO4, 18.02 grams of water, and 2.82 grams of dipropylamine (DPA) were added to a 100 ml teflon hned autoclave in the order hsted. The mixture was stirred to give a homogeneous solution. Next, 15.00 grams of dried extrudates (1/16" diameter) of the alumina bound SAPO-34 were added to the contents

in the autoclave. The extrudates were completely covered by the hquid. The molar composition of the synthesis mixture was:

DPA/AI2O3/P2O5/H2O of 0.76/0.75/1.0/30.9

In the mixture, the AI2O3 accounts for only the alumina binder of the extrudate and the P2O5 accounts for only the 85% aqueous H3PO4. The autoclave was sealed and heated in 2 hours to 200°C and held without stirring for 22 hours at 200°C. The autoclave was cooled to room temperature and the mother liquor was decanted. The extrudates were washed with de-ionized water until the conductivity of the filtrate was less than 100 micro-Siemens. XRD analysis showed typical patterns for both SAPO-34 and ALPO- 11.

EXAMPLE 6

Catalyst A and Catalyst B were tested for use in the conversion of oxygenates to olefins. The tests were carried out using the following procedure: 5.0 cc (approximately 2.7 grams) of each catalyst was mixed with 15 cc quartz beads and loaded into a 3/4" outer diameter 316 stainless steel tubular reactor which was heated by three-zone electric furnaces. The first zone acted as the preheating zone, vaporized the feed. The temperature of the center zone of the furnace was adjusted to 450°C and the pressure was maintained at 1 atm. The reactor was purged first with nitrogen at 50 cc/min flow rate for 30 minutes. The feed had a 4:1 molar ratio of water to methanol and was pumped into the reactor at a rate calibrated to give a flow rate of about 0.7hr ^] WHSV. The effluent was analyzed at pre-determined intervals by an on-hne gas chromatography fitted with both a thermal conductivity

detector and a flame ionization detector. The results of these tests are shown below in Table IV:

The data shows that the catalysts have good propylene selectivity and by tailoring the catalyst, product distribution can be varied.

EXAMPLE 7

A sample comprising 10 grams of the catalyst of Example 2 was loaded by ion exchange with a 0.6 wt percent palladium. The sample was exchanged using an aqueous mixture comprising 0.138 grams of Pd(NHs)2Cl2 and 9.62 grams of NH4NO3 which was dissolved in 100 cc of deminerahzed water. The pH of the mixture was adjusted to greater than 7 using a NH ₄ OH solution (30 wt.% NH ₃ ). This mixture, which contained the sample, was stirred for 24 hours at room temperature followed by two days without stirring at the same temperature. The Pd containing catalyst were then washed on a filter, oven dried at 90°C, and then calcined in air for 12 hours at 380°C.

Hydro-isomerization and hydro-cracking reactions were conducted. The tests were carried out by mixing two grams of the catalyst with 8 grams of quartz and then loading the catalyst into a 0.5 inch diameter stainless steel reactor. The total length of the reactor was 5 inches. The reactor was equipped with an axial thermo-well to measure the

actual bed temperature. Reduction was carried out for 1 hour at 716°F, pressure (psig) of 58, and a hydrogen flow rate (cc/min) of 184. After reduction, a n-hexane feed was introduced into the hydrogen stream to give a n-hexane weight hourly space velocity (WHSV) of 0.95 hrs. ¹ , a H2/n-hexane molar ratio of 20 and a total pressure of 58 psig. Product samples were recovered on-hne and analyzed by gas chromatography. The result of these tests are shown below in Table V.

TABLE V

(1) wt.% sum of 2,2 di-methyl-butane; 2,3 di-methyl-butane; 2-methyl-pentane; 3-methyl-pentane

(2) (yield branched hexanes/n-hexane conversion) x 100 (3) (yield Ci to Cc paraffins/n-hexane conversion) x 100

The data shows that the catalyst has high activity and high hydro- isomerization and hydrocracking selectivity.