This invention relates to a process for the catalytic disproportionation of toluene. Zeolitic materials, both natural and synthetic, have been demonstrated in the past to have catalytic properties for various types of hydrocarbon conversion. Certain zeolitic materials are ordered, porous crystalline aluminosilicates 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. These cavities and pores are uniform in size within a specific zeolitic material. Since the dimensions of these pores are such as to accept for adsorption molecules of certain dimensions while rejecting those of larger dimensions, these materials have come to be known as "molecular sieves" and are utilized in a variety of ways to take advantage of these properties. Such molecular sieves, both natural and synthetic, include a wide variety of positive ion-containing crystalline silicates. These silicates can be described as a rigid three-dimensional framework of SiO. and

Periodic Table Group IIIA element oxide, e.g., A10 ₄ , in which the tetrahedra are cross-linked by the sharing of oxygen atoms whereby the ratio of the total Group IIIA element, e.g., aluminum, and silicon atoms to oxygen atoms is 1:2. The electrovalence of the tetrahedra containing the Group IIIA element, e.g., aluminum, is balanced by the inclusion in the crystal of a cation, e.g., an alkali metal or an alkaline earth metal cation. This can be expressed wherein the ratio of the Group IIA element, e.g., aluminum, to the number of various cations, such as Ca/2, Sr/2, Na,

or Li, is equal to unity. One type of cation may be exchanged either entirely or partially with another type of cation utilizing ion exchange techniques in a conventional manner. By means of such cation exchange, it has been possible to vary the properties of a given silicate by suitable selection of the cation.

Prior art techniques have resulted in the formation of a great variety of synthetic zeolites. Many of these zeolites have come to be designated by letter or other convenient symbols, as illustrated by zeolite Z (U.S. Patent No. 2,882,243), zeolite X (U.S. Patent No. 2,882,244), zeolite Y (U.S. Patent No. 3,130,007), zeolite ZK-5 (U.S. Patent No. 3,247,195), zeolite ZK-4 (U.S. Patent No. 3,314,752), zeolite ZSM-5 (U.S. Patent No. 3,702,886), zeolite ZSM-11 (U.S. Patent No. 3,709,979), zeolite ZSM-12 (U.S. Patent No. 3,832,449), zeolite ZSM-20 (U.S. Patent No. 3,972,983), zeolite ZSM-35 (U.S. Patent No. 4,016,245), and zeolite ZSM-23 (U.S. Patent No. 4,076,842).

The S^/A^O _j ratio of a given zeolite is often variable. For example, zeolite X can be synthesized with SiO^/A^O _j ratios of from 2 to 3; zeolite Y, from 3 to 6. In some zeolites, the upper limit of the SiO^/A^O, ratio is unbounded. ZSM-5 is one such example wherein the S^/A^O _j ratio is at least 5 and up to the limits of present analytical measurement techniques. U.S. Patent No. 3,941,871 (Re. 29,948) discloses a porous crystalline silicate made from a reaction mixture containing no deliberately added alumina in the recipe and exhibiting the X-ray diffraction pattern characteristic of ZSM-5. U.S. Patent Nos. 4,061,724, 4,073,865 and 4,104,294 describe crystalline silicates of varying alumina and metal content. U.S. Patent Nos. 3,126,422; 3,413,374; 3,598,878; 3,598,879; and, 3,607,961 describe the vapor-phase disproportionation of toluene over various catalysts. U.S. Patent No. 4,117,026 discloses disproportionation of toluene over a catalyst comprising a zeolite having a silica/alumina mole ratio of at least 12, a Constraint Index of 1 to 12 and a specified sorption capacity for xylenes.

The present invention resides in a process for the disproportionation of toluene which comprises contacting toluene with a conversion catalyst comprising a zeolite having an X-ray diffraction pattern including the lines listed in Table I of the 5 specification.

The toluene feedstock employed in the present process is preferably dried to minimize water entering the reaction zone. Known methods for drying toluene are numerous, including percolation through silica gel, activated alumina, molecular sieves or other in suitable substances or the use of liquid charge dryers.

In addition to toluene, the feedstock employed in the present process may contain other aromatic hydrocarbons, include Cq+ aromatics. When present, the Cg aromatics may constitute up to 70 wt.% of the total feedstock.

^5 In general, the process of the invention can be conducted over a wide range of_ conversion conditions, including a temperature of 370°C to 595°C (700 to 1100°F), more preferably 413 to 540°C (775 to 1000°F), most preferably 427 to 510°C (800 to 950°F), a pressure of 100 to 7000 kPa (atmospheric to 1000 psig) , more preferably 1480

₂₀ to 7000 kPa (200 to 1000 psig), most preferably 2860 to 5620 kPa

(400 to 800 psig), a hydrogen to hydrocarbon mole ratio of 0 to 10, more preferably 0.25 to 5, most preferably 0.5 to 3 and a weight hourly space velocity of 0.16 to 30, preferably 0.5 to 15, most preferably 1 to 10.

₂₅ The catalyst employed in the present process includes a zeolite having, in its calcined form, an X-ray diffraction pattern including the lines listed in Table 1 below:

TABLE I

More specifically, the calcined form may be characterized by an X-ray diffraction pattern including tbe following lines:

TABLF II Interplanar d-Spacing (A) Relative Intensity, I/Io x IPO

30.0 W-M 22.1 .3 W 12.36 .4 M-VS 11.03 .2 M-S 8.83 .14 M-VS 6.86 .14 W-M 6.18 .12 M-VS 6.00 .10 W-M 5.54 .10 W-M 4.92 .09 W 4.64 .08 w 4.41 .08 W-M 4.25 .08 W 4.10 .07 w-s 4.06 .07 w-s 3.91 .07 M-VS 3.75 .06 W-M 3.56 .06 W-M 3.42 .06 VS 3.30 .05 W-M 3.20 .05 W-M 3.1^ .05 W-M 3.07 .05 W 2.99 .05 w 2.82 .05 w 2.78 .05 w 2.68 .05 w 2.59 .05 w

These values were determined by standard technicrues. The radiation was the K-alpha doublet of copper and a diffractometer equipped with a scintillation counter and an associated computer was used. The peak heights, I, and the positions as a function of 2 theta, where theta is the Bragg angle, were determined using algorithms on the computer associated with the diffractometer. From these, the relative intensities, 100 I/I , where I is the o o intensity of the strongest line or peak, and d (obs.) the interplanar spacing in Angstroms Units (A), corresponding to the recorded lines, were determined. In Tables I and II, the relative intensities are given in terms of the symbols W=weak, M=mediυτπ, S=strong and VS=very strong. In terms of intensities, these may be generally designated as follows:

W = 0 - 20

M = 20 - 40

S = 40 - 60

VS = 60 - 100 It should be understood that these X-ray diffraction patterns are characteristic of all species of the zeolite. The sodium form as well as other cationic forms of this zeolite reveal substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the Y to X, e.g., silicon to aluminum, mole ratio of the particular sample, as well as its degree of thermal treatment.

The zeolite de ined in Tables I and II generally has a composition involving the molar relationship:

X ₂ O ₃ :(n)Y0 ₂ , wherein X is a trivalent element, such as aluminum, boron, iron and/or gallium, preferably aluminum, Y is a tetravalent element such as silicon and/or germanium, preferably silicon, and n is at least

10, usually from 10 to 150, more usually from 10 to 60, and even more usually from 20 to 40. In the as-synthesized form, the zeolite has a formula, on an anhydrous basis and in terms of moles of oxides per n moles of Y0 , as follows:

(0.005-0.l)Na ₂ O:(l-4)R:X ₂ O ₃ :nY0 ₂ wherein R is an organic component. The Na and R components are associated with the zeolite as a result of their presence during crystallization, and are easily removed by post-crystallization methods hereinafter more particularly described.

The above zeolite is thermally stable and exhibits high

2 surface area (greater than 400 m /gm as measured by the BET

(Bruenauer, Emmet and Teller] test) and unusually large sorption capacity when compared to similar crystal structures. In particular, the zeolite exhibits equilibrium adsorption capacities greater than 4.5 wt.% for cyclohexane vapor, greater than 10 wt.% for n-hexane vapor and normally greater than 10 wt.% for water vapor. As is evident from the above formula, the zeolite is synthesized nearly free of Na cations. It can therefore be used as

a catalyst with acid activity without an exchange step. To the extent desired, however, the original sodium cations of the as-synthesized zeolite and the other zeolites useful in the present process can be replaced in accordance with techniques well known in the art, at least in part, by ion exchange with other cations. Preferred replacing cations include metal ions, hydrogen ions, hydrogen precursor, e.g., ammoniun, ions and mixtures thereof. Particularly preferred cations are those which tailor the catalytic activity for disproportionation. These include hydrogen, rare earth metals and metals of Groups IIA, IIIA, IVA, IB, IIB, IIIB, IVB and VIII of the Periodic Table of the Elements.

The zeolite defined in Tables I and II can be prepared from a reaction mixture containing sources of alkali or alkaline earth metal (M), e.g., sodium or potassium, cation, an oxide of trivalent element X, e.g, aluminum, an oxide of tetravalent element Y, e.g., silicon, an organic (R) directing agent in the form of hexamethyleneimine and water, said reaction mixture having a composition, in terms of mole ratios of oxides, within the following ranges: Reactants Useful Preferred

In a preferred synthesis method the Y0- reactant contains a substantial amount of solid Y0 ₂ , e.g., at least about 30 wt.% solid Y0 ₂ . Where Y0 ₂ is silica, the use of a silica source containing at least about 30 wt.% solid silica, e.g., Ultrasil (a precipitated, spray dried silica containing about 90 wt.% silica) or HiSil (a precipitated hydrated Si0 ₂ containing about 87 wt.% silica, about 6 wt.% free H ₂ 0 and about 4.5 wt.% bound H ₂ 0 of hydration and having a particle size of about 0.02 micron) favors

crystal formation from the above mixture. If another source of oxide of silicon, e.g., Q-Brand (a sodium silicate comprised of about 28.8 wt.% of Si0 ₂ , 8.9 wt.% Na ₂ 0 and 62.3 wt.% H ₂ 0) is used, crystallization may yield little if any of the desired crystalline material and impurity phases of other crystal structures may be produced. Preferably, therefore, the Y0 ₂ , e.g., silica, source contains at least about 30 wt.% solid Y0 ₂ , e.g., silica, and more preferably at least about 40 wt.% solid Y0 ₂ , e.g., silica. Crystallization can be carried out at either static or stirred conditions in a suitable reactor vessel such as, e.g., polypropylene jars or teflon-lined or stainless steel autoclaves. Suitable crystallization conditions include a temperature of 8 ^' 0°C to 225°C for a time of 25 hours to 60 days. Thereafter, the crystals are separated from the liquid and recovered. Synthesis is facilitated by the presence of at least about

0.01 percent, preferably about 0.10 percent and still more preferably about 1 percent, seed crystals (based on total weight) of the required crystalline product.

Prior the use in the process of the invention, the selected zeolite catalyst is preferably combined with another material which is resistant to the temperatures and other conditions employed in the process. Such materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials such as clays, silica and/or metal oxides such as alumina. The latter may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Use of a material in conjunction with the catalyst zeolite, i.e., combined therewith or present during its synthesis, which itself is catalytically active may change the conversion and/or selectivity of the catalyst. Inactive materials suitably serve as diluents to control the amount of conversion so that disproportionated products can be obtained economically and orderly without employing other means for controlling the rate of reaction. These materials may be incorporated into naturally

occurring clays, e.g., bentonite and kaolin, to irαprove the crush strength of the catalyst under commercial alkylation operating conditions. Said materials, i.e., clays, oxides, etc., function as binders for the catalyst. It is desirable to provide a catalyst having good crush strength because in commercial use, it is desirable to prevent the catalyst from breaking down into powder-like materials. These clay binders have been employed normally only for the purpose of improving the crush strength of the catalyst. Naturally occurring clays which can be composited with the zeolite catalyst herein include the montmorillonite and kaolin family, which families include the subbentonites, and the kaolins commonly known as Dixie, McNamee, Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite, or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification. Binders useful for compositing with zeolite also include inorganic oxides, notably alumina. In addition to the foregoing materials, the zeolite catalyst can be composited with a porous matrix material such as silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania as well as ternary compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina- magnesia and silica-magnesia-zirconia. It may also be advantageous to provide at least a part of the foregoing matrix materials in colloidal form so as to facilitate extrusion of the bound catalyst component(s).

The relative proportions of finely divided crystalline material and inorganic oxide matrix vary widely, with the crystal content ranging from 1 to 90 percent by weight and more usually, particularly when the composite is prepared in the form of beads, in the range of 2 to 80 weight percent of the composite.

The stability of the zeolite catalyst may be increased by steaming, which is conveniently effected by contacting the zeolite with, e.g., 5-100% steam at a temperature of at least 300°C (e.g., 300-650°C) for at least one hour (e.g., 1-200 hours) at a pressure of 100-2,500 kPa. In a more particular embodiment, the catalyst can be made to undergo steaming with 75-100% steam at 315-500°C and atmospheric pressure for 2-25 hours.

The invention will now be more fully described with reference to the following Examples and the accompanying drawings in which:

Figures 1-5 are X-ray diffraction patterns of the calcined . crystalline material products of Examples 1, 3, 4, 5 and 7, respectively.

In the Examples, whenever sorption data are set forth for comparison of sorptive capacities for water, cyclohexane and/or n-hexane, they were Equilibrium Adsorption values determined as ollows:

A weighed sample of the calcined adsorbent was contacted with the desired pure adsorbate vapor in an adsorption chamber, evacuated to less than 1 mm Hg and contacted with 1.6 kPa (12 Torr) of water vapor or 5.3 kPa (40 Torr) of n-hexane or 5.3 kPa (40 Torr) of cyclohexane vapor, pressures less than the vapor-liquid equilibrium pressure of the respective adsorbate at 90°C. The pressure was kept constant (within about + 0.5 mm Hjg) by addition of adsorbate vapor controlled by a manostat during the adsorption period, which did not exceed 8 hours. As adsorbate was adsorbed by the zeolite, the decrease in pressure caused the manostat to open a valve which admitted more adsorbate vapor to the chamber to restore the above control pressures. Sorption was complete when the pressure change was not sufficient to activate the manostat. The increase in weight was calculated as the adsorption capacity of the sample in g/100 g of calcined adsorbent.

When Alpha Value is examined, it is noted that the Alpha Value is an approximate indication of the catalytic cracking

activity of the catalyst compared to a standard catalyst and it gives the relative rate constant (rate of normal hexane conversion per volume of catalyst per unit time). It is based on the activity of a highly active silica-alumina cracking catalyst taken as an Alpha of 1 (Rate Constant ■ 0.016 sec ^"1 ). The Alpha Test which was used herein is described in J. Catalysis, 61, pp.390-396 (1980). It is noted that intrinsic rate constants for many acid-catalyzed reactions are proportional to the Alpha Value for a particular zeolite catalyst, i.e., the rates for toluene disproportionation, xylene isomerization, alkene conversion and methanol conversion (see "The Active Side of Acidic Aluminosilicate Catalysts," Nature, Vol. 309, No. 5969, pp. 589-591, 14 June 1984).

EXAMPLE 1 1 part of sodium aluminate (43.5% A1 ₂ 0 ₃ , 32.2% Na ₂ 0, 25.6% H ₂ 0) was dissolved in a solution containing 1 part of 50% NaOH solution and 103.13 parts H ₂ 0. To this was added 4.50 parts hexamethyleneimine. The resulting solution was added to 8.55 parts of Ultrasil, a precipitated, spray-dried silica (about 90% Si0 ₂ ).

The reaction mixture had the following composition, in mole ratios:

where R is hexamethyleneimine.

The mixture was crystallized in a stainless steel reactor, with stirring, at 150°C for 7 days. The crystalline product was filtered, washed with water and dried at 120°C. After a 20 hour calcination at 538°C, the X-ray diffraction pattern contained the major lines listed in Table III. Figure 1 shows the X-ray diffraction pattern of the calcined product. The sorption capacities of the calcined material were measured to be:

The surface area of the calcined crystalline material was measured to be 494 m /g.

The chemical composition of the uncalcined material was determined to be as follows:

Component wt.%

Si0 ₂ 66.9 A1 ₂ 0 ₃ 5.40

Na 0.03

N 2.27

Ash 76.3

Si0 ₂ /Al ₂ 0 ₃ , mole ratio - 21.1

4

PCT/US90/01923

13 -

TABLE III

A portion of the calcined crystalline product of Example 1 was tested in the Alpha Test and was found to have an Alpha Value of 224.

EXAMPLES 3-5 Three separate synthesis reaction mixtures were prepared with compositions indicated in Table VI. The mixtures were prepared with sodium aluminate, sodium hydroxide, Ultrasil, hexamethyleneimine (R) and water. The mixtures were maintained at 150°C, 143°C and 150°C, respectively, for 7, 8 and 6 days

- ,ir. ¬ PCT/US90/01923

respectively in stainless steel autoclaves at autogenous pressure. Solids were separated from any unreacted components by iltration and then water washed, followed by drying at 120°C. The product crystals were analyzed by X-ray diffraction, sorption, surface area and chemical analyses. The results of the sorption, surface area and chemical analyses are presented in Table IV and the X-ray diffraction patterns are presented in Figures 2, 3 and 4, respectively. The sorption and surface area measurements were of the calcined product. TABLE IV

FXAMPLF 6 Quantities of the calcined (538°r for hours) crystalline silicate products of Examples 3, 4 and 5 were tested in the Alpha Test and found to have Alpha Values of 227, 180 and 187, respectively.

EXAMPLF 7 To demonstrate a further preparation of the present zeolite, 4.49 parts of hexamethyleneimine was added to a solution containing 1 part of sodium aluminate, 1 part of 50% NaOF solution and 44.19 parts of H-0. To the combined solution were added 8.5^ parts of Ultrasil silica. The mixture was crystallized with agitation at 145°C for 59 hours and the resultant product was water washed and dried at 120°C.

The X-ray diffraction pattern of the dried product crystals is presented in Figure 5. Product chemical composition, surface area and adsorption analyses results were as set forth in Table :

TABLE V Product Composition (uncalcined)

C 12.1 wt.% N 1.98 wt.%

Na 640 ppm

A1 ₂ 0 ₃ 5.0 wt.%

Si0 ₂ 74.9 wt.%

Si0 ₂ /Al ₂ 0 ₃ , mole ratio 25.4

Adsorption, wt.%

Cyclohexane 9.1

N-Hexane 14.9

H ₂ 0 16.8

2 Surface Area, m /g 479

EXAMPLE 8 25g grams of solid crystal product from Example 7 were calcined in a flowing nitrogen atmospheres at 538°C for 5 hours, followed by purging with 5% oxygen gas (balance N ₂ ) for another 16 hours at 538°C.

Individual 3g samples of the calcined material were ion-exchanged with 100 ml of 0.1N TEABr, TPABr and LaCl ₃ solution separately. Each exchange was carried out at ambient temperature for 24 hours and repeated three times. The exchanged samples were collected by filtration, water-washed to be halide-free and dried. The compositions of the exchanged samples are tabulated below.

Exchange Ions TEA TPA La

Ionic C

The La-exchanged sample from Example 8 was sized to 14 to 25 mesh and then calcined in air at 538°C for 3 hours. The calcined material had an Alpha Value of 173.

EXAMPLE 10 The calcined sample La-exchanged material from Example 9 was severely steamed at 649°C in 100% steam for 2 hours. The 5 steamed sample had an Alpha Value of 22, demonstrating that the zeolite had very good stability under severe hydrothermal treatment.

EXAMPLE 11 This example illustrates the preparation of the present zeolite where X in the general formula, supra, is boron. Boric Q acid, 2.59 parts, was added to a solution containing 1 part of 45% KOH solution and 42.96 parts H ₂ 0. To this was added 8.56 parts of Ultrasil silica, and the mixture was thoroughly homogenized. A 3.88 parts quantity of hexamethyleneimine was added to the mixture.

P T

- 17 -

The reaction mixture had the following composition in mole ratios:

Si0 ₂ /B ₂ 0 ₃ = 6.1 , 0H7Si0 ₂ = 0.06 H ₂ 0/Si0 ₂ = 19.0

K/Si0 ₂ = 0.06

R/Si0 ₂ = 0.30 where R is hexamethyleneimine.

The mixture was crystallized in a stainless steel reactor, with agitation, at 150°C for 8 days. The crystalline product was filtered, washed with water and dried at 12P°r. A portion of the product was calcined for 6 hours at 540°C and found to have the following sorptipn capacities:

H ₂ 0 11.7 wt.% Cyclohexane 7.5 yrt.% n-Hexane 11.4 wt.%

The surface area of the calcined crystalline material was measured (BET) to be 405m ² /g.

The chemical composition of the uncalcined material was determined to be as follows:

N 1.94 wt.%

Na 175 ppm

K 0.60 wt.%

Boron 1.04 wt.% ^A1 2°3 ⁹²⁰ PP" ¹

Si0 ₂ 75.9 wt.%

Ash 74.11 wt.%

Si0 ₂ /Al ₂ 0 ₃ , molar ratio = 1406 Si0 ₂ /(A1+B) ₂ 0 ₃ , molar ratio = 25.8

EXAMPLE 12

A portion of the calcined crystalline product of Fxa ple 11 was treated with NH ₄ C1 and again calcined. The final crystalline product was tested in the Alpha Test and found to have an Alpha Value of 1.

EXAMPLE 13 This example illustrates another preparation of the zeolite in which X of the general formula, supra, is boron. Boric acid, 2.23 parts, was added to a solution of 1 part of 50% NaOH solution and 73.89 parts HJ). To this solution was added 15.29 parts of HiSil silica followed by 6.69 parts of hexamethyleneimine. The reaction mixture had the following composition in mole ratios:

where R is hexamethyleneimine.

The mixture was crystallized in a stainless steel reactor, with agitation, at 300°C for 9 days. The crystalline product was filtered, washed with water and dried at 120°C. The sorption capacities of the calcined material (6 hours at 540°C) were measured: H ₂ 0 14.4 wt.%

Cyclohexane 4.6 wt.% n-Hexane 14.0 wt.%

The surface area of the calcined crystalline material was measured to be 438m /g.

The chemical composition of the uncalcined material was determined to be as follows:

EXAMPLE 14 A portion of the calcined crystalline product of Example 13 was tested in the Alpha Test and found to have an Alpha Value of 5.

EXAMPLES 15 and 16

These examples can have the results otained in the disproportionation of toluene using the zeolite of the invention (Example 15) of those obtaining using ZSM-5 (Example 16).

The zeolite of the invention was prepared by adding 4.49 parts hexamethyleneimine to a mixture containing 1.00 part sodium aluminate, 1.00 part 50% NaOH, 8.54 parts Ultrasil VN3 and 44.19 parts deionized H ₂ 0. The reaction mixture was heated to 143°C (290°F) and stirred in an autoclave at that temperature for crystallization. After full crystallinity was achieved, the majority of the hexamethyleneimine was removed from the autoclave by controlled distillation and the zeolite crystals separated from the remaining liquid by filtration, washed with deionized H 0 and dried. A 65 wt.% zeolite/35 wt.% A1 ₂ 0 catalyst composition was prepared from the zeolite by extrusion. The material was then dried overnight at 120°C (250°F), calcined at 480°C (900°F) for three hours in 3v/v/min N ₂ , then treated with 50 vol.% air/50 vol.% N ₂ at 3v/v/min, also at 480°C (900°F) for one hour. The calcination was completed by raising the temperature to 540°C (1000°F) at 3°C (5°F)/min and finally switching to 100% air (3v/v/min) and holding at this temperature for three hours. A similar process was used to prepare the ZSM-5 catalyst.

The properties of the zeolite catalyst compositions are set forth in Table VI as follows:

TABLE VI

Zeolite of Tables I-IV ZSM-5

Alpha Value 215 194

2 Surface area, m /g 451 349

Each of the experiments was started at 4240 kPa (600 psig), 4 hr -~1 ^x weight hourly space velocity (based on zeolite) and a hydrogen/hydrocarbon mole ratio of 2. The toluene feedstock was passed over the catalyst in each instance at a temperature required to maintain 45 +_ 3 wt.% toluene conversion. The results are given in Table VII.

Days on Stream Temperature, °F (°C) Toluene Conversion, wt%

Aging Rate, °F/Day (°C/day)

Product Distribution, wt%

C5 ^"

Benzene Toluene

Ethylbenzene p-Xylene m-Xylene o-Xylene C9+

The above results indicate that the zeolite of the invention exhibited a greater catalyst activity and a lower aging rate than ZSM-5. The combination of these factors will result in significantly longer cycle lengths with the catalyst of the invention.