Preparation of a dimethyltetralin

Abstract: 5-Tolylpent-1- or -2-ene or 5-phenylhex-1- or -2-ene is transformed in a dimethyltetraline by passing it in liquid form over a zeolite y. Isomers of dimethylnaphtalene can be obtained by subsequent dehydrogenation and isomerisation of the produced dimethyltetraline.

Description: This invention relates generally to a method for preparing a dimethyltetralin and more particularly concerns a method for preparing primarily a specific dimethyltetralin or a mixture of specific dimethyltetralins from either 5-(o-, m-, or p-tolyl)- pent-1- or -2-ene or 5-phenyl-hex-1- or -2-ene in the presence of a Y-type crystalline aluminosilicate molecular sieve zeolite. Description of the Prior Art Naphthalene dicarboxylic acids are monomers that are known to be useful for the preparation of a variety of polymers. For example, poly(ethylene 2,6-naphthalate) prepared from 2,6-naphthalene dicarboxylic acid and ethylene glycol has better heat resistance and mechanical properties than polyethylene terephthalate and is useful in the manufacture of films and fibers. Dimethylnaphthalenes are desirable feedstocks for oxidation to the corresponding naphthalene dicarboxylic acids. A known conventional process for producing a naphthalene dicarboxylic acid comprises the oxidation of a dimethylnaphthalene with oxygen in the liquid phase in an acetic acid solvent at an elevated temperature and pressure and in the presence of a catalyst comprising cobalt, manganese and bromine components. Typically dimethylnaphthalenes are found in refinery or coal-derived streams as mixtures of all of the ten possible dimethylnaphthalene isomers. However, separation of these isomers is very difficult and expensive. Consequently, methods for producing specific dimethylnaphthalenes or mixtures of two or three specific dimethylnaphthalenes in high purity and quality are highly desirable. One type of such method is a multistep synthesis involving (1) the formation of an alkenylbenzene by the reaction of o-, m- or p-xylene or ethylbenzene with butadiene, (2) the cyclization of the resulting alkenylbenzene to form one or more dimethyltetralins belonging to one or two of three groups of three isomeric dimethyltetralins -- that is, either group A containing the 1,5-, 1,6-, 2,5- and 2,6-dimethyltetralins, group B containing the 1,7-, 1,8-, 2,7- and 2,8-dimethyltetralins, or group C containing the 1,3-, 1,4-, 2,3-, 5,7-, 5,8- and 6,7-dimethyltetralins -- (3) the dehydrogenation of the dimethyltetralin(s) to form the corresponding dimethylnaphthalene(s), and (4) the isomerization of the resulting dimethylnaphthalene(s) to the desired specific dimethylnaphthalene. For example, Thompson, U.S. Patents Nos. 3,775,496; 3,775,497; 3,775,498; 3,775,500 disclose processes for the cyclization of specific alkenylbenzenes to one or more specific dimethyltetralins at 200-450°C in the presence of any suitable solid acidic cyclization catalyst such as acidic crystalline zeolites as well as silica-alumina, silica-magnesia and silica-alumina-zirconia and phosphoric acid, followed by the dehydrogenation of the resulting dimethyltetralin(s) in the vapor state to the corresponding dimethylnaphthalene(s) in a hydrogen atmosphere at 300-500°C and in the presence of a solid dehydrogenation catalyst such as noble metals on carriers and chromia-alumina, and thereafter isomerization of each of the aforesaid dimethylnaphthalene(s) to the desired isomer within the triad of dimethylnaphthalenes to which the isomer being isomerized belongs, at 275-500°C in the presence of a solid acidic isomerization catalyst of the same type as described in respect of the cyclization disclosed therein. In the alternative, both the cyclization and isomerization reactions can be performed in the liquid phase, in which case the cyclization is performed at 200-275°C with a solid phosphoric acid catalyst, at 70-140°C with an acidic ion exchange resin, an acidic crystalline zeolite, hydrofluoric or sulfuric acid as the catalyst or a siliceous cracking catalyst. More specifically, Thompson, U.S. Patent No. 3,775,496 discloses the cyclization of 5-(m-tolyl) -pent-2-ene to 1,6- and 1,8-dimethyltetralins, which are then dehydrogenated to 1,6- and 1,8-dimethylnaphthalenes, which in turn are isomerized to 2,6- and 2,7-dimethylnaphthalenes, respectively. Thompson, U.S. Patent No. 3,775,497 discloses the cyclization of 5-phenyl-hex-2-ene to 1,4-dimethyltetralin which is then dehydrogenated to 1,4-dimethylnaphthalene, which is in turn isomerized to 2,3-dimethylnaphthalene. Thompson, U.S. Patent No. 3,775,498 discloses the cyclization of 5-(o-tolyl)-pent-2-ene to 1,5-dimethyltetralin, which is then dehydrogenated to 1,5-dimethylnaphthalene, which is in turn isomerized to 2,6-dimethylnaphthalene. Thompson, U.S. Patent No. 3,775,500 discloses the cyclization of 5-(p-tolyl)-pent-2-ene to 1,7-dimethyltetralin, which is then dehydrogenated to 1,7-dimethylnaphthalene, which in turn is isomerized to 2,7-dimethylnaphthalene. Shimada et al., U.S. Patent No. 3,780,119 disclose a method for the isomerization of dimethylnaphthalene by the use at a temperature above 260°C of a mordenite catalyst in which a metal form of mordenite is in excess of 20 weight percent of the mordenite, with the metal being selected from the group consisting of lithium, sodium, potassium, magnesium, calcium, strontium, barium, zinc and aluminum. Suld et al., U.S. Patent No. 3,803,253 disclose a method for the hydroisomerization of a dimethylnaphthalene by the use of a combination of a hydrogenation catalyst and a calcium-containing zeolite catalyst, such as a calcium-exchanged synthetic faujasite, for example, a Y-type molecular sieve. JP 48-96577 A discloses a process for producing dimethyltetralins using a Y-type zeolite, teaching that gas-phase reaction conditions are preferable, but does not address the problem of maintain catalyst life without carrying out the reaction under conditions that reduce product yield. Shima et al., U.S. Patent No. 3,806,552 disclose a method for the isomerization of dimethylnaphthalenes in the gas phase by the use of a mixed catalyst consisting of (a) 65-95 weight percent of a hydrogen form of mordenite in which above 80 weight percent of the metal cations are replaced with hydrogen ions, and (b) 5-35 weight percent of catalyst selected from the group consisting of bentonite and fuller's earth. Hedge, U.S. Patent No. 3,855,328 discloses a method for the isomerization of dimethylnaphthalenes by the use of a Type Y alumino silicate zeolite at 120-300°C in the liquid phase. The catalysts have aluminum-to-silicon atomic ratios of 0.1-1.0. Ogasawara et al., U.S. Patent No.3,888,938 disclose a method for the isomerization of dimethylnaphthalenes in the liquid phase by the use of a mixed catalyst consisting of (a) 70-95 weight percent of a hydrogen form of mordenite in which above 80 weight percent of the metal cations are replaced with hydrogen ions, and (b) 5-30 weight percent of a promoter selected from the group consisting of bentonite and fuller's earth. Hedge et al., U.S. Patent No. 3,928,482 disclose the isomerization of either dimethyldecalins, dimethyltetralins or dimethylnaphthalenes in the presence of an alumino silicate zeolite containing polyvalent metal cations in exchange positions, such as a rare earth-exchanged Type Y zeolite. Yokayama et al., U.S. Patent No. 3,957,896 disclose the selective isomerization of dimethylnaphthalenes in the presence of any kind of natural or synthetic, solid acid catalyst, such as Y-type zeolite as well as silica-alumina, silica-magnesia, silica-zirconia, silica-alumina-zirconia, fuller's earth, natural or synthetic mordenite, X-type zeolite, A-type zeolite and L-type zeolite. These catalysts may be substituted partly or wholly by hydrogen or metal. Furthermore, these catalysts can be unsupported or supported on carriers. Onodera et al., U.S. Patent No. 4,524,055 disclose a crystalline aluminosilicate zeolite that is useful in the isomerization of dimethylnaphthalenes and has a silica-to-alumina mole ratio of 10 to 100, specific x-ray lattice distances, and a specific cyclohexane-to-n-hexane adsorption ratio of at least 0.7. Maki et al., U.S. Patent No. 4,556,751 disclose the isomerization of dimethylnaphthalenes in the presence of a crystalline aluminosilicate having a pentasil structure and a silica-to-alumina molar structure of 12 or higher. In addition, the aluminosilicate may contain some other metals as non-exchangeable metals. A problem in all such prior art methods is the presence of other dimethylnaphthalene isomers and unconverted dimethyltetralin and alkenylbenzene as impurities and by-products in the finally obtained, desired specific dimethylnaphthalene isomer. The presence of such impurities and by-products markedly reduces the utility and commercial value of the desired dimethylnaphthalene isomer, especially as a precursor for the formation of a naphthalene dicarboxylic acid for use as a monomer in the manufacture of a polymer. In addition, catalysts tend to deactivate relatively rapidly at the high temperatures employed in vapor phase processes. Therefore, it is highly desirable to employ relatively lower temperature liquid phase processes and to improve the completeness of each step in the aforesaid multistep synthesis and the selectivity of each step therein for the production of the desired product therefrom. In this regard, it is known that in the presence of an acid catalyst, the dimethylnaphthalene isomers are isomerizable within each triad of dimethylnaphthalene isomers -- that is, within the 1,5-, 1,6- and 2,6-dimethylnaphthalenes of triad A, within the 1,7-, 1,8-, and 2,7-dimethylnaphthalenes of triad B, and within the 1,3-, 1,4- and 2,3-dimethylnaphthalenes of triad C. It is also known that the interconversion of a dimethylnaphthalene isomer within one of the aforesaid triads to a dimethylnaphthalene isomer within another of the aforesaid triads occurs to a relatively lesser extent. Consequently, it is highly desired to improve the selectivity of the cyclization step in the aforesaid multistep synthesis for the formation of dimethyltetralin isomers that belong to the same triad to which also belongs the specific desired dimethyltetralin isomer, which upon dehydrogenation is converted to the desired specific corresponding dimethylnaphthalene isomer. It is also highly desired to improve the selectivity and completeness of the isomerization step in the aforesaid multistep synthesis for the formation of the specific dimethylnaphthalene isomer desired. OBJECTS OF THE INVENTION It is therefore a general object of the present invention to provide an improved method for manufacturing with an improved yield and selectivity a specific dimethyltetralin isomer or set of dimethyltetralin isomers by the cyclization of an alkenylbenzene which meets the aforementioned requirements for selectivity and completeness and catalyst activity. It is a related object of the present invention to provide an improved method for manufacturing with an improved yield and selectivity a specific dimethylnaphthalene isomer or set of dimethylnaphthalene isomers by the cyclization of an alkenylbenzene to form a specific dimethyltetralin isomer or set of dimethyltetralin isomers and then dehydrogenating the dimethyltetralin(s). It is another related object of the present invention to provide an improved method for manufacturing with an improved yield and selectivity a specific dimethylnaphthalene isomer or set of specific dimethylnaphthalene isomers by the cyclization of an alkenylbenzene to form a specific dimethyltetralin isomer or set of dimethyltetralin isomers and then dehydrogenating the dimethyltetralin(s) and isomerizing the resulting dimethylnaphthalene(s). Other objects and advantages of the method of the present invention will become apparent upon reading the following detailed description and appended claims. SUMMARY OF THE INVENTION The objects are achieved by an improved method for preparing a dimethyltetralin from 5-(o-, m-, or p-tolyl)-pent-1- or -2-ene or 5-phenyl-hex-1- or -2-ene as the first feedstock, comprising: contacting the first feedstock in liquid form with a solid cyclization catalyst comprising a Y-type, crystalline aluminosilicate molecular sieve zeolite that is substantially free of adsorbed water, and at an elevated temperature and at a pressure that is sufficiently high to maintain the first feedstock substantially in the liquid phase, to thereby cyclize the first feedstock to form a first liquid product comprising a mixture of dimethyltetralins, wherein, if present, the concentration of water in the first feedstock is less than about 0.5 weight percent, based on the weight of the feedstock, wherein either (a) the first feedstock comprises 5-(o-tolyl)-pent-1- or -2-ene and 1,5-, 1,6-, 2,5- or 2,6-dimethyltetralin or mixtures thereof comprise at least 80 weight percent of the mixture of dimethyltetralins formed, (b) the first feedstock comprises 5-(m-tolyl)-pent-1- or -2-ene and 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6-, 2,7-, or 2,8-dimethyltetralin, or mixtures thereof comprise at least 80 weight percent of the mixture of dimethyltetralins formed, (c) the first feedstock comprises 5-(p-tolyl)-pent-1- or -2-ene and 1,7-, 1,8-, 2,7-, or 2,8-dimethyltetralin, or mixtures thereof comprise at least 80 weight percent of the mixture of dimethyltetralins formed, (d) the first feedstock comprises 5-phenyl-1- or -2-hexene and 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethyltetralin or mixtures thereof comprise at least 80 weight percent of the mixture of dimethyltetralins formed. BRIEF DESCRIPTION OF THE DRAWING For a more complete understanding of this invention, reference should now be made to the embodiments illustrated in greater detail by the results presented in the accompanying drawing and described below by way of examples of the invention. In the drawing, FIG. 1 is a series of plots of the yields of 1,5-dimethyltetralin from the cyclization of 5-o-tolyl-2-pentene in Examples 19-23 involving 5 different cyclization catalysts. DETAILED DESCRIPTION OF THE PREFERRED EMBODIMENTS Suitable feedstocks for use in the cyclization of the method of the present invention are 5-(o-, m-, or p-tolyl)-pent-1- or -2-ene or 5-phenyl-hex-1- or -2-ene. In the method of the present invention, the cyclization step is followed preferably by a dehydrogenation step and more preferably by first a dehydrogenation step and second an isomerization step. When 5-(o-tolyl)-pent-1- or -2-ene is the feedstock to the cyclization step of the present invention, 1,5-, 1,6-, 2,5-, or 2,6-dimethyltetralin or a mixture thereof comprises at least 80, preferably at least 85 weight percent of the dimethyltetralins produced therefrom, which resulting dimethytetralins are in turn the feedstock and are converted in the dehydrogenation step of the present invention to the corresponding 1,5-, 1,6- and 2,6-dimethylnaphthalenes, which are then the feedstock in the isomerization step of the present invention and are converted therein to 2,6-dimethylnaphthalene. When 5-(m-tolyl)-pent-1- or -2-ene is the feedstock to the cyclization step, 1,5- 1,6- 1,7-, 1,8- 2,5- 2,6-, 2,7- or 2,8-dimethyltetralin or a mixture thereof comprises at least 80, preferably at least 85 weight percent of the dimethyltetralins produced therefrom, which dimethyltetralins are in turn the feedstock and are converted in the dehydrogenation step to the corresponding 1,5-, 1,6-, 1,7-, 1,8- 2,6- and 2,7-dimethylnaphthalenes, which are then the feedstock in the isomerization step and are converted to 2,6- and 2,7-dimethylnaphthalenes. When 5-(p-tolyl)-pent-1- or -2-ene is the feedstock to the cyclization step, 1,7-, 1,8-, 2,7- or 2,8-dimethyltetralin or a mixture thereof comprises at least 80, preferably at least 85 weight percent of the dimethyltetralins produced therefrom, which dimethyltetralins are in turn the feedstock and are converted in the dehydrogenation step to the corresponding 1,7-, 1,8- and 2,7-dimethylnaphthalenes which are then the feedstock and are converted in the isomerization step to 2,7-dimethylnaphthalene. When 5-phenyl-1- or -2-hexene is the feedstock to the cyclization step, 1,3-, 1,4-, 2,3-, 5,7, 5,8-, or 6,7-dimethyltetralin or a mixture thereof comprises at least 80, preferably at least 85 weight percent of the dimethyltetralins produced therefrom, which dimethyltetralins are in turn the feedstock and are converted in the dehydrogenation step to the corresponding, 1,3-, 1,4- and 2,3-dimethylnaphthalenes, which are then the feedstock in the isomerization step and are converted to 2,3-dimethylnaphthalene. In the method of the present invention, each of the aforesaid cyclization, dehydrogenation and isomerization reactions is performed in the liquid phase at an elevated temperature and at a sufficiently high pressure to ensure that the feedstock for the particular step is maintained substantially in the liquid phase. The cyclization reaction is performed at a temperature in the range of from 120°C, preferably from 150°C, to 250°C, preferably to 230°C, and generally at a pressure in the range of from 0.1, preferably from 0.3, to 5, preferably to 1.3, atmospheres absolute (30.4 to 506, preferably to 132 kPa). The dehydrogenation reaction is performed at a temperature in the range of from 200°C, preferably from 220°C, to 300°C, preferably to 270°C, and generally at a pressure in the range of from 0.5, preferably from 0.8, to 5, preferably to 1.3 atmospheres absolute (51, preferably 80 to 506, preferably 132. The isomerization reaction is performed at a temperature in the range of from 200°C, preferably from 240°C, to 300°C, preferably to 280°C, and generally at a pressure in the range of from 0.5, preferably from about 0.8, to 5, preferably to 1.3 atmospheres absolute. (51, preferably 80 to 506, preferably 132 kPa). Each of the cyclization, dehydrogenation and isomerization reactions can be performed with or without a solvent for the respective feedstock. Preferably a solvent is not employed in the aforesaid steps. If employed, a solvent in any of the aforesaid steps must be inert under the conditions employed and suitably comprise a paraffin such as a tetradecane, or an aromatic hydrocarbon such as anthracene, or mixtures thereof, which preferably boils above 270°C. In the cyclization step, if water is present, its concentration is less than 0.5 weight percent, preferably less than 0.1 weight percent, based on the weight of the alkenylbenzene feedstock. More preferably, water is not present in the cyclization reaction medium. Each of the cyclization, dehydrogenation and isomerization steps of the method of the present invention can be performed either batchwise or continuously. The reaction apparatus to be used in each aforesaid step can be of any known type such as a fixed bed, moving bed, fluidized bed, liquid phase suspended bed or a solid-liquid mixture in a stirred tank. Generally, however, the use of a fixed bed is commercially preferred for continuous operation. The improved conversion of the feedstock and selectivity for the production of the desired product or set of products for each of the cyclization, dehydrogenation and isomerization steps of the method of this invention are the result of the temperature and pressure conditions employed and the high activity and selectivity of the catalysts employed in each aforesaid step, which in turn permits the use of less severe conditions -- that is, lower temperatures and pressures --such that greater selectivity and reduced catalyst deactivation can be achieved. The catalyst employed in the cyclization step of the method of this invention comprises an acidic ultrastable -- that is, a thermally stabilized or dealuminated --Y-type crystalline aluminosilicate zeolite having a silica-to-alumina molar ratio of from 4:1, preferably from 5:1, to 10:1, preferably to 6:1, and having pore windows provided by twelve-membered rings containing oxygen, and a unit cell size of from 24.2, preferably from 24.3, to 24.7, preferably to 24.6 angstroms. A suitable such zeolite is marketed by Union Carbide under the name LZ-Y72 or LZ-Y20. The zeolite is preferably substantially free of adsorbed water. If present on the zeolite, the adsorbed water can be removed from the zeolite by heating it in a dry atmosphere at 250°C for 0.5-1 hour. In the alternative, and less preferably, the presence of absorbed water at a concentration of up to 15 weight percent of the catalyst can be tolerated if a reaction temperature in the aforesaid range of at least 180°C is employed. The aforesaid zeolite employed in the catalyst for the cyclization step of the method of this invention is in the hydrogen form and contains from 0.05, up to 3.5 weight percent of sodium, calculated as elemental sodium and based on the weight of the zeolite. If the cyclization step is performed batchwise, the cyclization catalyst preferably contains from 1 to 3.5 weight percent of sodium, calculated as elemental sodium and based on the weight of the zeolite. If the cyclization step is performed continuously, the cyclization catalyst preferably contains from 0.05 to 0.5 weight percent, calculated as elemental sodium and based on the weight of the zeolite. Preferably, the cyclization catalyst contains from 0.01, preferably from 0.05, to 3, preferably to 1.5 weight percent of a component comprising a first metal selected from the group consisting of platinum, palladium, iridium and rhodium, calculated as the elemental metal and based on the weight of the catalyst. Most preferably this metal component comprises platinum. More preferably, especially when the cyclization is performed continuously, the cyclization catalyst also contains from 0.01, preferably from 1, to 5, preferably to 3 weight percent of a component comprising a second metal selected from the group consisting of copper, tin, gold, lead and silver, calculated as the elemental metal and based on the weight of the catalyst. More preferably this second metal component comprises copper, tin or gold. The aforesaid zeolite can be employed either unsupported or supported on a porous refractory, inorganic oxide that is inert under the conditions employed, such as silica, alumina, silica-alumina, magnesia, bentonite or other such clays. If a support is employed, preferably the support comprises silica, alumina, or silica-alumina. When a support is employed, the zeolite comprises from 10, preferably from 20, to 90, preferably to 80 weight percent based on the weight of the catalyst. If the cyclization is performed on a batch basis, the catalyst is employed at a level in the range of from 0.1, preferably from 1.0, to 5, preferably to 3 weight percent of the zeolite component of the catalyst, based on the weight of the alkenylbenzene feedstock, and the reaction time is from 0.5, preferably from 2, to 10, preferably to 6 hours. If the cyclization is performed on a continuous basis, the space velocity is in the range of from 0.1, preferably from about 1, to 10, preferably to 5, parts of alkenylbenzene feedstock per part of zeolite component of the catalyst by weight per hour. The catalyst employed in the dehydrogenation step of the method of this invention is any solid dehydrogenation catalyst that is capable of effecting the dehydrogenation and exhibiting a reasonable lifetime under the conditions employed, including catalysts such as noble metals on carriers such as reforming catalysts. Preferably, palladium on an active carbon or alumina support containing from 0.5, more preferably from 1.0, to about 15, more preferably to 10 weight percent of palladium, calculated as elemental palladium and based on the weight of the catalyst, is employed as the dehydrogenation catalyst. If the dehydrogenation is performed on a batch basis, the catalyst is employed at a level in the range of from 0.005, preferably from 0.01, to 1.0, preferably to 0.2 weight percent of the noble metal component, calculated as the elemental noble metal and based on the weight of the dimethyltetralin feedstock, and the reaction time is from about 1, preferably from 2, to 20, preferably to 10 hours. If the dehydrogenation is performed on a continuous basis, the space velocity is in the range of from 0.1, preferably from 10, to 100, preferably to 50 parts of the dimethyltetralin feedstock per part of the noble metal component (calculated as the elemental noble metal) of the catalyst by weight per hour. The catalyst employed in the isomerization step of the method of this invention comprises either beta zeolite or an acidic ultrastable -- that is, a thermally stabilized or dealuminated -- Y-type crystalline aluminosilicate zeolite having a silica-to-alumina molar ratio of from 4:1 preferably from 5:1, to 10:1, preferably to 6:1, and having pore windows provided by twelve-membered rings containing oxygen, and a unit cell size of from 24.2, preferably from 24.3, to 24.7, preferably to 24.6 angstroms. A suitable such zeolite is marketed by Union Carbide under the name LZ-Y72 or LZ-Y20. Water is not detrimental to catalytic activity or selectivity in the isomerization process. The isomerization catalyst preferably comprises beta zeolite. The composition, structure and preparation of beta zeolite are described in Wadlinger et al., U.S. Patent No. 3,308,069 which in its entirety is specifically incorporated herein by reference. The structure of beta zeolite is also reported in J. Haggin, "Structure of Zeolite Beta Determined," in Chemical & Engineering News, p. 23 (June 20, 1988). Beta zeolite is also commercially available from PQ Corporation. The aforesaid ultrastable Y-type zeolite which can be employed in the catalyst for the isomerization step of the method of this invention is in the hydrogen form and contains from 0.01, preferably from 1, up to 5, preferably up to 3, weight percent of sodium, calculated as elemental sodium and based on the weight of the zeolite. Preferably the isomerization catalyst comprises a hydrogenation component comprising a Group VIII metal, which more preferably is palladium, platinum or nickel. The aforesaid zeolite of the isomerization catalyst can be employed either unsupported or supported on a porous refractory, inorganic oxide that is inert under the conditions employed, such as silica, alumina, silica-alumina, magnesia, bentonite or other such clays. If a support is employed, preferably the support comprises silica, alumina or silica-alumina. When a support is employed, the zeolite comprises from 10, preferably from 20, to 90, preferably to 80 weight percent based on the weight of the catalyst. If the isomerization is performed on a batch basis, the catalyst is employed at a level in the range of from 0.1, preferably from 1.0, to 5, preferably to 3 weight percent of the zeolite component of the catalyst, based on the weight of the dimethylnaphthalene feedstock, and the reaction time is from 0.5, preferably from 2, to 10, preferably to 6 hours. If the isomerization is performed on a continuous basis, the space velocity is in the range of from 0.1, preferably from 0.5 to 10, preferably to 5 parts of dimethylnaphthalene feedstock per part of zeolite component of the catalyst by weight per hour. The present invention will be more clearly understood from the following specific examples. EXAMPLES 1-8 In each of Examples 1-8, 20-1000 grams of an alkenylbenzene were introduced into a stirred glass reactor, and dry nitrogen gas was employed to continuously purge the reaction medium to preclude moisture therefrom. The alkenylbenzene employed was 5-(o-tolyl)-pentene-2 in Examples 1-6, 5-(p-tolyl)-pentene-2 in Example 7 and 4-phenyl-pentene-2 in Example 8. Unsupported ultrastable Y-type crystalline aluminosilicate molecular sieve catalyst (union Carbide's LZ-Y72) having a unit cell size of 24.51Å and containing 2.5 weight percent of sodium (calculated as sodium oxide) were added slowly to the alkenylbenzene in the reactor at a temperature below commencement of the cyclization of the alkenylbenzene. The catalyst was in the form of an unsupported powder in Examples 1-4, 7 and 8, and in the form of pellets containing 80 weight percent of the same sieve supported on 20 weight percent of an alumina support in Examples 5 and 6. The catalyst was maintained under dry, moisture-free conditions prior to use in Examples 1-3 and 5-8 but was allowed to adsorb moisture from air saturated with moisture at 30-60°C in Example 4. The catalyst employed in Example 4 contained 10-20 weight percent of water. The temperature of the reaction medium was then raised quickly to the desired reaction time. Samples of the resulting reaction product were withdrawn from the reactor at various reaction times and analyzed to monitor the reaction. The desired cyclized product was 1,5-dimethyltetralin in Examples 1-6, 1,7-dimethyltetralin in Example 7 and 1,4-dimethyltetralin in Example 8. The experimental conditions employed, the compositions of the feedstock employed and of the resulting products containing up to 13 carbon atoms and the percent conversion of the alkenylbenzene feedstock, and the percent selectivity of the formation of desired product from the total amount of alkenylbenzene converted for each of Examples 1-8 are presented in Table 1. For the calculation of this percent selectivity, the desired product is the sum of 1,5-dimethyltetralin and 1,5-dimethylnaphthalene in Examples 1-6, the sum of 1,7-dimethyltetralin and 1,7-dimethylnaphthalene in Example 7, and the sum of 1,4-dimethyltetralin and 1,4-dimethylnaphthalene in Example 8. Comparison of the results of Examples 2 and 4 illustrates that, even at the low feed-to-catalyst weight ratio employed in Example 4, the presence of a large concentration of water therein resulted in substantially reduced percents conversion, even after a reaction time of about 12 hours. EXAMPLES 9-23 In each of Examples 9-23, a cyclization catalyst was packed into a stainless steel reaction, and the reactor was immersed into a fluidized sand bath at the desired reaction temperature. A mixture of 5-o-tolyl-2-pentene in the liquid phase and nitrogen was passed continuously through the reactor. At least once during at least one catalyst cycle, the resulting product stream was sampled and analyzed. The experimental conditions employed, the compositions of the feedstock employed and of the resulting products containing up to 13 carbon atoms, the percent conversion of the alkenylbenzene feedstock, and the percent selectivity of the formation of desired product from the total amount of alkenylbenzene converted in each of Examples 9-23 are presented in Table 2. A catalyst cycle was concluded by discontinuing the flow of the 5-o-tolyl-2-pentene into the reactor and then purging the reactor at the reaction temperature with nitrogen to remove the hydrocarbons. The reactor was next heated to 500°C and purged with air until the carbon dioxide content of the reactor effluent was less than 0.1 weight percent. This procedure resulted in the regeneration of the catalyst. The reactor was then cooled to the desired reaction temperature, and then the mixture of 5-o-tolyl-2-pentene in the liquid phase and nitrogen was passed continuously into the reactor. In each of Examples 9-12 and 19-23, the reactor had an outside diameter of 0.635 cm (0.25 inch), an inside diameter of 0.457 cm (0.18 inch), a length of 13.97 cm (5.5 inch), and one gram of the catalyst was packed into the reactor. In each of Examples 13-18, the reactor had an outside diameter of 0.952 cm (0.375 inch), an inside diameter of 0.71 cm (0.28 inch), a length of 12.7 cm (5 inch), and 2.5 grams of the catalyst were packed into the reactor. In each of Examples 9-14, an unsupported ultra-stable Y-sieve containing platinum and copper components was employed. This catalyst was prepared by adding to 30 grams of the commercial ultra-stable Y-sieve (Union Carbide's LZ-Y20) 15 milliliters of distilled water and 30 grams of an aqueous solution containing 1 weight percent of H₂PtCl₆·6H₂O), calculated as platinum, and 2 weight percent of copper in the form of cupric nitrate and calculated as elemental copper. The resulting slurry was mixed until it was uniform and then dried. The resulting solid was calcined at 500°C in air for 4 hours, crushed and screened to obtain 0.0164-0.0278 inch (24-40 mesh) particles. In each of Examples 15-18, a supported ultra-stable Y-sieve containing platinum and copper components was employed. This catalyst was prepared by crushing and screening a commercial sample of particles containing 80 weight percent of Union Carbide's LZ-Y20 supported on 20 weight percent of alumina to yield particles in the range of 24-40 mesh. To 10 grams of the supported sieve was added 11 milliliters of 0.9 weight percent of H₂PtCl₆, calculated as platinum, and 1.8 weight percent of copper in the form of cupric nitrate, calculated as elemental copper. The resulting slurry was mixed until it was uniform and then dried. The resulting solid was calcined at 500°C in air for 4 hours. Each of Examples 19-23 was performed using the apparatus and procedure of Examples 9-12 at a reaction temperature of 154°C and a space velocity of 1.1. The diluent gas was helium in Examples 19 and 20, hydrogen in Examples 21 and 22 and nitrogen in Example 23. The molar ratio of diluent-to-5-o-tolyl-2-pentene was 1.3 in Example 19 and 2.1 in each of Examples 20-23. The catalyst was unsupported in each example, and was ultra-stable Y-sieve (Union Carbide's LZ-Y20) in Example 19, ultra-stable Y-sieve containing 2 weight percent of copper in the form of cupric nitrate, (calculated as elemental copper) in each of Examples 20 and 21, ultra-stable Y-sieve treated with SiCl₄ in Example 22 and ultra-stable Y-sieve containing 2 weight percent of copper in the form of cupric nitrate (calculated as elemental copper) and 1 weight percent of platinum in the form of H₂PtCl₆ (calculated as elemental platinum) in Example 23. In each of Examples 19-23, samples of the product stream were taken at several times after the beginning of the catalyst cycle and analyzed. From these measurements the yields of 1,5-dimethyltetralin were calculated and in Figure 1 are plotted versus the number of hours since the respective catalyst had been regenerated. The results indicate that the addition of copper to the sieve or the treatment of the sieve with silicon tetrachloride improves the selectivity of the catalyst but that the catalytic activity decreases with time. However, the addition of both platinum and copper to the sieve affords both substantially improved selectivity and excellent catalyst activity maintenance. EXAMPLES 24-29 In each of Examples 24-29, the liquid feed and a 5 weight percent palladium-on-carbon catalyst were charged to a flask and nitrogen was continuously passed through the reaction mixture to remove oxygen. The temperature of the reaction mixture was raised to the reaction temperature, and periodically samples were removed from the flask and analyzed. Hydrogen generated by the reaction was permitted to vent from the flask during the reaction. The experimental conditions employed, the compositions of the feedstock employed and of the resulting products containing up to 13 carbon atoms, the percent conversion of the feedstock, and the percent selectivity of the formation of desired product from the total amount of feedstock converted in each of Examples 24-29 are presented in Table 3. The results in Table 3 illustrate that even with the mild temperature and pressure conditions employed in Examples 24-29, the dehydrogenation of the method of this invention affords both excellent conversion and selectivity. EXAMPLES 30-47 In each of Examples 30-47, the particular isomer of dimethylnaphthalene employed as the feed was mixed in liquid form with unsupported catalyst in a stirred reaction vessel with a continuous nitrogen purge to preclude oxygen from the system. The temperature of the reaction vessel was raised to the reaction temperature and samples were withdrawn at various times after commencement of the reaction and analyzed. The conditions employed, the compositions of the feedstock employed and of the resulting products containing up to 13 carbon atoms, the percent conversion of the feedstock, and the percent selectivity of the formation of desired product from the total amount of feedstock converted in each of Examples 30-47 are presented in Table 4. The catalyst employed in Example 30 was a crystalline borosilicate molecular sieve (HAMS-1B from Amoco Chemical). The catalyst employed in Example 31 was Union Carbide's LZ-Y20 ultra-stable Y-type sieve, containing 2 weight percent of copper, calculated as elemental copper. The catalyst employed in Example 32 was Union Carbide's LZ-Y62, a non-ultra-stable, Y-type sieve in the ammonia-exchanged form and having a unit cell size of 24.73Å. The catalyst employed in Examples 33 and 34 was commercially available Union Carbide's LZ-Y82, an ultra-stable molecular sieve having a unit cell size of 24.56Å and a sodium content of less than 0.2 weight percent. In Example 33, the sieve was in the ammonia form and had not been calcined. In Example 34, the sieve had been calcined to form the hydrogen form. The catalyst employed in Example 35 was a commercially available amorphous silica-alumina containing 13 weight percent of alumina. The catalyst employed in Example 36 was commercially available mordenite in the acid form. The catalyst employed in Examples 37, 38, 40-45 was commercially available Union Carbide's LZ-Y72 in the hydrogen form as received from the manufacturer. The catalyst employed in Example 39 was commercially available Grace USY sieve containing 2.6 weight percent of sodium and has chemical and physical properties that are very similar to those of Union Carbide's LZ-Y72, and is also suitable for use as a catalyst in either the cyclization or isomerization step in the method of this invention. 1,5-dimethylnaphthalene was the feed in Examples 30-44. The feed was 1,7-dimethylnaphthalene in Example 45 and 1,4-dimethylnaphthalene in Examples 46 and 47. For the purposes of Table 4, the concentration of 2,7-DMN in the product is taken to be approximately equal to the concentration of 1,7-DMN and is subtracted from the sum of 2,6-DMN and 2,7-DMN (which are determined together) for the purpose of determining the concentration of 2,6-DMN alone. The effective maximum concentrations of a particular desired DMN in its triad is its equilibrium concentration in the triad, which generally is 40-45 weight percent. EXAMPLE 48 7.5 kilograms of distilled water, 7.5 kilograms of an aqueous solution containing 40 weight percent of tetraethylamine hydroxide, 50 grams of sodium hydroxide and 300 grams of sodium aluminate were stirred and dissolved in a 94.6 litre (25-gallon) stainless steel tank. The resulting solution and 12.2 kilograms of a silica sol containing 40 weight percent of silica were mixed and stirred in a 37.9 litre (10 gallon) autoclave at 150°C for 72 hours. The resulting mixture was filtered, and the separated solids were washed three times with distilled water, dried at 120°C and then calcined at 538°C for 4 hours. The resulting dried powder contained 0.37 weight percent of sodium, calculated as elemental sodium, and x-ray diffraction analysis indicated that the powder had the x-ray diffraction pattern of beta zeolite. The following is the x-ray diffraction pattern of the powder product, showing only the lines that are common to all 4 sources of beta zeolite in U.S. Patent No. 3,308,069. Line d(A) Relative Intensity 4.18 16.2 3.99 100.0 3.54 6.1 3.35 12.6 3.11 3.0 3.05 14.6 2.94 5.3 2.69 4.1 2.54 1.5 2.08 11.5 The powder was employed as the catalyst without being ion-exchanged. Some powder was ion-exchanged using the procedure of Example 50 to reduce the sodium content, and after being ion-exchanged, the powder's alumina content, silica-to-alumina mole ratio and silicon-to-aluminum atom ratio were measured as 1.14 weight percent, 68:1 and 34:1, respectively. EXAMPLE 49 8 kilograms of distilled water, 8 kilograms of an aqueous solution containing 40 weight percent of tetraethylamine hydroxide, 3.81 kilograms of an aqueous solution containing 20 weight percent of tetraethylamine hydroxide, 0.6 kilogram of sodium aluminate, and 12.2 kilograms of a silica sol containing 40 weight percent of silica were mixed and stirred in a 10-gallon (38 ℓ) autoclave at 150°C for 72 hours. The resulting mixture was filtered, and the separated solids were washed three times with distilled water, dried at 120°C for about 16 hours and then calcined at 538°C for 6 hours. The resulting dried powder contained 0.17 weight percent of sodium, calculated as elemental sodium. X-ray diffraction analysis indicated that the powder had the x-ray diffraction pattern of beta zeolite. The following is the x-ray diffraction pattern of the powder product, showing only the lines that are common to all 4 sources of beta zeolite in U.S. Patent No. 3,308,069. Line d(A) Relative Intensity 4.19 17.7 4.01 100.0 3.54 Weak 3.35 13.8 3.11 Weak 3.05 13.4 2.95 2.8 2.67 Weak 2.49 0.6 2.09 7.6 The powder was employed as the catalyst without being ion-exchanged. After being ion-exchanged using the procedure of Example 50 in order to reduce the sodium content, the powder's silica-to-alumina mole ratio and silicon-to-aluminum atom ratio were measured as 30:1 and 14.8:1, respectively. EXAMPLE 50 2.3 kilograms of the un-ion-exchanged catalyst powder produced in Example 49, 4 kilograms of distilled water, and 12 kilograms of an aqueous solution containing 19 weight percent of ammonium nitrate were stirred in a 22-liter flask at 72°C for 4 hours. The mixture was then cooled; the liquid was removed by decantation, and the resulting ion-exchanged catalyst was then washed with water. The catalyst was then dried at 120°C and calcined at 538°C for 3 hours. The ion-exchanged catalyst contained 0.01 weight percent of sodium (calculated as elemental sodium), 2.43 weight percent of aluminum (calculated as elemental aluminum), and a silica-to-alumina mole ratio and a silicon-to-aluminum atomic ratio of 30:1 and 14.8:1, respectively. 163 grams of this dry, ion-exchanged beta zeolite powder, 454 grams of an alumina sol containing 8.8 weight percent of solids, and 123 grams of distilled water were blended to obtain a smooth, uniform slurry. The slurry was maintained at 23°C for 5 hours to permit liquid to evaporate from the slurry. The slurry was then dried at 120°C for about 16 hours and calcined at 538°C for 2 hours, to afford solids containing 80 weight percent of beta zeolite and 20 weight percent of alumina, which were then ground and sieved to form particles having a 20-40 mesh size. EXAMPLES 51-69 In each of Examples 51-69, the particular feedstock employed was mixed in liquid form with unsupported catalyst in a stirred reaction vessel with a continuous nitrogen purge to preclude oxygen from the system. The weight ratio of the feedstock-to-zeolite component of the catalyst was 49:1 in each case. The pressure of the contents of the reaction vessel was maintained at about 1 pound per square inch gauge. The temperature of the reaction vessel was raised to the reaction temperature and samples were withdrawn at various times after commencement of the reaction and analyzed. The conditions employed, the compositions of the feedstock employed and of the resulting products, the percent of the 1,5-, 1,6- and 2,6-DMN triad in each thereof, the percent of 2,6-DMN in each such 1,5-, 1,6- and 2,6-DMN triad, the percent decreases in each 1,5-, 1,6- and 2,6-DMN triad, the percent gains in each 1,7-, 1,8- and 2,7-DMN triad and the percent gain in total methylnaphthalene and trimethylnaphthalene content in each of Examples 51-69 are presented in Tables 5-9. The catalyst employed in Examples 51-53 was commercially available Union Carbide's unsupported LZ-Y72 in the hydrogen form as received from the manufacturer. The catalyst employed in Examples 54-57 was an unsupported beta zeolite having a relatively high silicon-to-aluminum ratio and prepared by the procedure of Example 48. The catalyst employed in Examples 58-66 was an unsupported beta zeolite having a relatively low silicon-to-aluminum ratio and prepared by the procedure of Example 49. A single sample of this catalyst was used for four cycles in Examples 61-66. The catalyst employed in Examples 67-70 was also the beta zeolite having the relatively low silicon-to-aluminum ratio and prepared by the procedure of Example 49, but in this instance ion-exchanged to reduce the sodium content and supported on an alumina matrix by the procedure of Example 50. Comparison of the results in Tables 5-9 illustrates clearly that (1) the use of a beta zeolite catalyst affords reduced losses of the 1,5-, 1,6- and 2,6-dimethylnaphthalene triad, reduced formation of methylnaphthalenes, trimethylnaphthalenes and the 1,7-, 1,8- and 2,7-dimethylnaphthalene triad relative to the use of the LZ-Y72 zeolite catalyst; and (2) the use of a beta zeolite catalyst either unsupported or supported on a base material and having a relatively lower silicon-to-aluminum ratio affords greater formation of 2,6-dimethylnaphthalene and reduced losses of the 1,5-, 1,6- and 2,6-dimethylnaphthalene triad relative to the use of a beta zeolite catalyst having a relatively higher silicon-to-aluminum ratio and permits the use of lower reaction temperatures or the use at a higher temperature of even a partially deactivated catalyst relative to the use of a LZ-Y72 zeolite catalyst. From the above description, it is apparent that the objects of the present invention have been achieved.

Claims: A method for preparing a dimethyltetralin from 5-(o-, m-, or p-tolyl)-pent-1- or -2-ene or 5-phenyl-hex-1-or -2-ene as feedstock (first feedstock), comprising: contacting the first feedstock in liquid form with a solid cyclization catalyst comprising an ultrastable Y-type, crystalline aluminosilicate molecular sieve zeolite that has a silica-to-alumina molar ratio of from 4:1 to 10:1, pore windows provided by twelve-membered rings containing oxygen and a unit cell size of from 24.2 x 10⁻¹⁰ to 24.7 x 10⁻¹⁰m (24.2 to 24.7 angstroms), and is substantially free of adsorbed water, and at an elevated temperature and at a pressure that is sufficiently high to maintain the first feedstock substantially in the liquid phase, to thereby cyclize the first feedstock to form a first liquid product comprising a mixture of dimethyltetralins, wherein, if present, water is at a concentration in the first feedstock of less than about 0.5 weight percent, based on the weight of the feedstock, wherein either (1) the first feedstock comprises 5-(o-tolyl)-pent-1-or -2-ene, and 1,5-, 1,6-, 2,5- or 2,6-dimethyltetralin, or a mixture thereof, comprises at least 80 weight percent of the mixture of dimethyltetralins formed, (2) the first feedstock comprises 5-(m-tolyl)-pent-1- or -2-ene, and 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6-, 2,7-, and 2,8-dimethyltetralin, or a mixture thereof, comprises at least 80 weight percent of the mixture of dimethyltetralins formed, (3) the first feedstock comprises 5-(p-tolyl)-pent-1- or -2-ene, and 1,7-, 1,8-, 2,7- or 2,8-dimethyltetralin, or a mixture thereof, comprises at least 80 weight percent of the mixture of dimethyltetralins formed, or (4) the first feedstock comprises 5-phenyl-hex-1-or -2-ene, and 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethyltetralin or a mixture thereof, comprises at least 80 weight percent of the mixture of dimethyltetralins formed. The method of Claim 1 wherein the cyclization is performed at a temperature in the range of from 150°C to 230°C. The method of Claim 1 or Claim 2 wherein the cyclization catalyst contains from 0.05 up to 3.5 weight percent of sodium calculated as elemental sodium, and based on the weight of the zeolite. The method of Claim 3 wherein the Y-type molecular sieve zeolite is in the hydrogen form and contains from 0.05 to 3 weight percent of a noble metal component selected from the group consisting of platinum, palladium, iridium, and rhodium, calculated as the elemental metal, and on the basis of the weight of the cyclization catalyst. The method of Claim 4 wherein the cyclization catalyst also comprises from 0.01 to 5 weight percent of a component comprising a transition metal selected from the group consisting of copper, tin, gold, lead and silver, calculated as the elemental metal and based on the weight of the catalyst. The method of any preceding claim wherein the cyclization catalyst is free of a support material. The method of any of Claims 1 to 5 wherein the cyclization catalyst is supported on an inert, porous refractory, inorganic oxide support material. The method of any preceding claim wherein the cyclization catalyst employed in the cyclization contains less than 15 weight percent of water adsorbed thereon based on the weight of the zeolite component thereof. The method of Claim 1 wherein additionally a mixture of dimethylnaphthalenes is formed, comprising: contacting the first liquid product from Claim 1 as a second feedstock in liquid form with a solid dehydrogenation catalyst in a reaction vessel at an elevated temperature and at a pressure that is sufficiently high to maintain the second feedstock substantially in the liquid phase, to thereby effect conversion of the aforesaid first liquid product in an equilibrium dehydrogenation reaction to form hydrogen and a second liquid product comprising a mixture of dimethylnaphthalenes, and removing a substantial portion of the hydrogen being formed in the dehydrogenation reaction from the reaction vessel to thereby shift the aforesaid equilibrium toward the formation of the mixture of dimethylnaphthalenes, wherein either (a) 1,5-, 1,6-, 2,5-, or 2,6-dimethyltetralin or a mixture thereof comprises at least 80 weight percent of the dimethyltetralins formed in (1) of Claim 1 are present in the second feedstock, and 1,5-, 1,6- or 2,6-dimethylnaphthalene or a mixture thereof comprises at least 80 weight percent of the dimethylnaphthalenes in the second liquid product, or (b) 1,5-, 1,6-, 1,7-, 1,8-, 2,5-, 2,6-, 2,7-, or 2,8-dimethyltetralin or a mixture thereof comprises at least 80 weight percent of the dimethyltetralins formed in (2) of Claim 1 are present in the second feedstock, and 1,5-, 1,6-, 1,7-, 1,8-, 2,6-, or 2,7-dimethylnaphthalene, or a mixture thereof comprises at least 80 weight percent of the dimethylnaphthalenes in the second liquid product, or (c) 1,7-, 1,8-, 2,7- or 2,8-dimethyltetralin or a mixture thereof comprises at least 80 weight percent of the dimethyltetralins formed in (3) of Claim 1 are present in the second feedstock, and 1,7-, 1,8- or 2,7-dimethylnaphthalene or a mixture thereof comprises at least 80 weight percent of the dimethylnaphthalenes in the second liquid product; or (d) 1,3-, 1,4-, 2,3-, 5,7-, 5,8- or 6,7-dimethyltetralin or a mixture thereof comprises at least 80 weight percent of the dimethyltetralins formed in (4) of Claim 1 are present in the second feedstock, and 1,3-, 1,4- or 2,3-dimethylnaphthalenes or a mixture thereof comprises at least 80 weight percent of the dimethylnaphthalenes in the second liquid product. The method of Claim 9 wherein the dehydrogenation is performed at a temperature in the range of from 220°C to 270°C. The method of Claim 10 wherein the dehydrogenation is performed at a pressure in the range of from 0.5 to 5 atmospheres absolute (51 to 507 kPa). The method of any of Claims 9 to 11 wherein the dehydrogenation catalyst comprises a noble metal component supported on a substantially inert support material, with the noble metal component employed at a level of from 0.5 to 15 weight percent, calculated as the elemental noble metal and based on the weight of the dehydrogenation catalyst. The method of any of Claims 9 to 12 wherein additionally there is isomerized at least 20 weight percent of the total of either (A) the 1,5- and 1,6-dimethylnaphthalenes in the second liquid product in (a) of Claim 9 to 2,6-dimethylnaphthalene, (B) the 1,5-, 1,6-, 1,7- and 1,8-dimethylnaphthalenes in the aforesaid second liquid product in (b) of Claim 9 to 2,7-dimethylnaphthalene and to 2,6-dimethylnaphthalene, (C) the 1,7- and 1,8-dimethylnaphthalenes in the aforesaid second liquid product in (c) of Claim 9 to 2,7-dimethylnaphthalene, or (D) the 1,3- and 1,4-dimethylnaphthalene in the aforesaid second liquid product in (d) of Claim 9 to 2,3-dimethylnaphthalene, comprising: contacting the aforesaid second liquid product in liquid form with a solid isomerization catalyst comprising either beta zeolite or an acidic ultrastable Y-type crystalline zeolite having a silica-to-alumina molar ratio of from about 4:1 to about 10:1, and having pore windows provided by twelve-membered rings containing oxygen and a unit cell size of from about 24.2 to about 24.7 angstroms, and at an elevated temperature and at a pressure that is sufficiently high to maintain the isomerization feedstock substantially in the liquid phase. The method of Claim 13 wherein at least 25 weight percent of the total dimethylnaphthalenes specified in alternatives (A), (B), (C) and (D) are isomerised to the products referred to. The method of Claim 13 or Claim 14 wherein the isomerization is performed at a temperature in the range of from 240°C to 280°C. The method of any of Claims 13 to 15 wherein the isomerization catalyst employed comprises beta zeolite. The method of any of Claims 13 to 16 wherein the isomerization catalyst comprises a hydrogenation component comprising a Group VIII metal. The method of any of Claims 13 to 17 wherein the isomerization catalyst employed is free of a support material. The method of any of Claims 13 to 17 wherein the isomerization catalyst is supported on an inorganic support material. A method according to any preceding claim wherein the cyclisation is performed at a temperature in the range of from 120°C to 250°C. A method according to any of Claims 9 to 20 wherein the dehydrogenation is performed at a temperature in the range of from 200°C to 300°C. A method according to any of Claims 13 to 21 wherein the isomerisation is performed at a temperature in the range of from 200°C to 300°C.

Inventors: LAMB JOYCE DALE, SIKKENGA DAVID LEE, WILLIAMS GREGORY SCOTT, ZAENGER IAN CLAYTON, LAMB, JOYCE DALE, SIKKENGA, DAVID LEE, WILLIAMS, GREGORY SCOTT, ZAENGER, IAN CLAYTON
Applicants: AMOCO CORP, AMOCO CORPORATION
Application year: 1989
Main classification: C07C13
IPC codes: C07C13, B01J29, C07B61, C07C5, C07C15