Process for preparing dimethylnaphthalene

Abstract: In a process for producing 2,6-dimethylnaphthalene an alkylaromatic compound, e.g. toluene, is alkylated with a C₅ olefin alkylating agent, e.g. 1-pentene, in the presence of a zeolite alkylation catalyst having a Constraint Index not greater than 5, and the resulting alkylate is dehydrocyclized with a dehydrocyclization catalyst to generate a dimethylnaphthalene product rich in the 2,6-isomer.

Description: This invention relates to a process for preparing dimethylnaphthalene. The compound 2,6-dimethyl naphthalene is a high value commodity chemical that is used in the manufacture of polymers and polyester resins. Up to now, some of the methods for producing dimethylnaphthalene have required expensive starting materials such as 4-pentenyl-toluene; 5-(o-tolyl)-pent-2-ene; and 1,3-dimethyl-4-isobutylbenzene. Thus U.S. Patent No. 3,775,496 describes a multistep process for the preparation of 2,6-dimethylnaphthalene and 2,7-dimethylnaphthalene from 5-0-tolyl-pentene-2. The 5-0-tolyl-pentene-2 is first converted to a mixture of 1,6- and 1,8-dimethyltetralins, which are then dehydrogenated to the respective dimethylnaphthalenes. The dimethylnaphthalenes (DMN) are then isomerized respectively to 2,6-dimethylnaphthalene and 2,7-dimethylnaphthalene. U.S. Patent No. 4,795,847 discloses a process for the preparation of 2,6-dialkylnaphthalenes by selectively alkylating naphthalene or 2-alkyl-naphthalene with an alkylating agent such as methanol in the presence of a zeolite ZSM-5 catalyst. U.S. Patent No. 4,777,312 describes a method for isomerization of a feedstock of mixed dimethylnaphthalenes to produce a higher concentration of 2,6-dimethylnaphthalene isomer than in the feedstock. This method employs mordenite type zeolite as a catalyst. EP-A-362507 describes a process for producing 2,6-dimethylnaphthalene by reacting toluene with n-butene and carbon monoxide, then hydrogenating the carbonyl group of the resultant p-tolyl sec-butyl ketone and then subjecting the hydrogenated product to dehydrogenation and cyclization. The present invention resides in a process for producing dimethylnaphthalene from a feedstock containing toluene and a C₅ olefin, said process comprising the steps of: a) contacting said feedstock with an alkylation catalyst composition to produce an alkylate, said catalyst composition comprising a synthetic crystalline zeolite having a Constraint Index not greater than 5, and then b) contacting said alkylate with a dehydrocyclization catalyst to produce a product containing dimethylnaphthalene. Specifically, the process described herein can generate a product rich in 2,6-dimethylnaphthalene when the feedstock is toluene and the alkylating olefin is 1-pentene. The product also can contain naphthalene, monomethylnaphthalene, and other isomers of dimethylnaphthalene. Optional additional processes can include isomerizing the dimethylnaphthalenes in the product to increase the fraction of the 2,6-isomer, and alkylating the naphthalene and monomethyl-naphthalene with methanol in the presence of the above alkylation catalyst to produce dimethylnaphthalene, including the 2,6-isomer. The first step in the process of the invention involves alkylating an alkylaromatic feedstock, preferably toluene, with a C₅ olefin alkylating agent, preferably 1-pentene, in the presence of a synthetic crystalline zeolite having a Constraint Index not greater than 5, preferably not greater than 3. Constaint Index and the method by which it is determined is described in U.S. Patent No. 4,016,218. Constraint Index (CI) values for some typical zeolites including some which are suitable as catalysts in the alkylation step of this invention are: Some zeolite catalysts which are useful in the process of this invention include zeolites ZSM-4, ZSM-12, ZSM-20, ZSM-35, ZSM-48, ZSM-50, TMA offretite, TEA mordenite, clinoptilolite, mordenite, REY and zeolite Beta. Of these, zeolites ZSM-12 and Beta are preferred. Zeolite ZSM-4 is taught in British Patent No. 1,117,568; ZSM-12 in U.S. Patent No. 3,832,449; ZSM-20 in U.S. Patent No. 3,972,983; ZSM-35 in U.S. Patent No. 4,016,245; ZSM-48 in U.S. Patent No. 4,397,827; ZSM-50 in U.S. Patent No. 4,640,849; and Beta in U.S. Patent No. 3,308,069. More preferably, the zeolite employed in the alkylation step of the process of the invention has, in its calcined form, an X-ray diffraction pattern including the following lines: Interplanar d-Spacing (A) Relative Intensity, I/I o x 100 12.36 ± 0.4 M-VS 11.03 ± 0.2 M-S 8.83 ± 0.14 M-VS 6.18 ± 0.12 M-VS 6.00 ± 0.10 M-M 4.06 ± 0.07 W-S 3.91 ± 0.07 M-VS 3.42 ± 0.06 VS or more specifically, the following lines: Interplanar d-Spacing (A) Relative Intensity, I/I o x 100 30.0 ± 2.2 W-M 22.1 ± 1.3 W 12.36 ± 0.4 M-VS 11.03 ± 0.2 M-S 8.83 ± 0.14 M-VS 6.18 ± 0.12 M-VS 6.00 ± 0.10 W-M 4.06 ± 0.07 W-S 3.91 ± 0.07 M-VS 3.42 ± 0.06 VS or alternatively, the following lines: Interplanar d-Spacing (A) Relative Intensity, I/I o x 100 12.36 ± 0.4 M-VS 11.03 ± 0.2 M-S 8.83 ± 0.14 M-VS 6.86 ± 0.14 W-M 6.18 ± 0.12 M-VS 6.00 ± 0.10 W-M 5.54 ± 0.10 W-M 4.92 ± 0.09 W 4.64 ± 0.08 W 4.41 ± 0.08 W-M 4.25 ± 0.08 W 4.10 ± 0.07 W-S 4.06 ± 0.07 W-S 3.91 ± 0.07 M-VS 3.75 ± 0.06 W-M 3.56 ± 0.06 W-M 3.42 ± 0.06 VS 3.30 ± 0.05 W-M 3.20 ± 0.05 W-M 3.14 ± 0.05 W-M 3.07 ± 0.05 W 2.99 ± 0.05 W 2.82 ± 0.05 W 2.78 ± 0.05 W 2.68 ± 0.05 W 2.59 ± 0.05 W or most specifically, the following lines: Interplanar d-Spacing (A) Relative Intensity, I/I o x 100 30.0 ± 2.2 W-M 22.1 ± 1.3 W 12.36 ± 0.4 M-VS 11.03 ± 0.2 M-S 8.83 ± 0.14 M-VS 6.86 ± 0.14 W-M 6.18 ± 0.12 M-VS 6.00 ± 0.10 W-M 5.54 ± 0.10 W-M 4.92 ± 0.09 W 4.64 ± 0.08 W 4.41 ± 0.08 W-M 4.25 ± 0.08 W 4.10 ± 0.07 W-S 4.06 ± 0.07 W-S 3.91 ± 0.07 M-VS 3.75 ± 0.06 W-M 3.56 ± 0.06 W-M 3.42 ± 0.06 VS 3.30 ± 0.05 W-M 3.20 ± 0.05 W-M 3.14 ± 0.05 W-M 3.07 ± 0.05 W 2.99 ± 0.05 W 2.82 ± 0.05 W 2.78 ± 0.05 W 2.68 ± 0.05 W 2.59 ± 0.05 W The values in Tables A-D were determined by standard techniques, using as radiation the K-alpha doublet of copper. The diffractometer employed was equipped with a scintillation counter and the peak heights, I, and the positions as a function of 2 theta, where theta is the Bragg angle, were determined using algorithms on a computer associated with the diffractometer. From these, the relative intensities, 100 I/I o , where I o is the intensity of the strongest line or peak, and d (obs.) the interplanar spacing in Angstrom Units (A), corresponding to the recorded lines, were determined. In Tables A-D, the relative intensities are given in terms of the symbols W=weak, M=medium, S=strong, 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 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 ratio of structural components, e.g., silicon to aluminum mole ratio of the particular sample, as well as its degree of thermal treatment. Examples of zeolites which, in their calcined form, have an x-ray diffraction pattern with the lines listed in Table A include the PSH-3 composition of U.S. Patent No. 4,439,409, and MCM-22 as disclosed in U.S. Patent No. 4,954,325. Zeolite MCM-22 has a composition involving the molar relationship: X₂O₃:(n)YO₂, 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, zeolite MCM-22 has a formula, on an anhydrous basis and in terms of moles of oxides per n moles of YO₂, as follows: (0.005-0.1)Na₂O:(1-4)R:X₂O₃:nYO₂ wherein R is hexamethyleneimine. 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. Zeolite MCM-22 is thermally stable and exhibits a high surface area greater than about 400m²/gm as measured by the BET (Bruenauer, Emmet and Teller) test. As is evident from the above formula, MCM-22 is synthesized nearly free of Na cations and thus possesses acid catalysis activity as synthesized. It can, therefore, be used as a component of the catalyst composition herein without having to first undergo an exchange step. To the extent desired, however, the original sodium cations of the as-synthesized material can be replaced in accordance with techniques well known in the art, at least in part, by ion exchange with other cations. Preferred replacement cations include metal ions, hydrogen ions, hydrogen precursor, e.g., ammonium, ions and mixtures thereof. Preferred cations are those which tailor the activity of the catalyst for alkylation. 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. In its calcined form, zeolite MCM-22 appears to be made up of a single crystal phase with little or no detectable impurity crystal phases and has an X-ray diffraction pattern including the lines listed in above Tables A-D. Zeolite MCM-22 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, hexamethyleneimine, and water, said reaction mixture having a composition, in terms of mole ratios of oxides, within the following ranges: Reactants Useful Preferred YO₂/X₂O₃ 10 - 60 10 - 40 H₂O/YO₂ 5 - 100 10 - 50 OH⁻/YO₂ 0.01 - 1.0 0.1 - 0.5 M/YO₂0 .01 - 2.0 0.1 - 1.0 R/YO₂ 0.05 - 1.0 0.1 - 0.5 In a preferred method of synthesizing zeolite MCM-22, the YO₂ reactant contains a substantial amount of solid YO₂, e.g., at least about 30. wt.% solid YO₂. Where YO₂ 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 SiO₂ containing about 87 wt.% silica, about 6 wt.% free H₂O and about 4.5 wt.% bound H₂O of hydration) favors MCM-22 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 SiO₂, 8.9 wt.% Na₂O and 62.3 wt.% H₂O) is used, crystallization may yield impurity phases of other crystal structures, e.g., ZSM-12. Preferably, therefore, the YO₂, e.g., silica, source contains at least about 30 wt.% solid YO₂, e.g., silica, and more preferably at least about 40 wt.% solid YO₂, e.g., silica. Crystallization of the MCM-22 crystalline material 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. Crystallization is conveniently conducted at a temperature of 80 to 225°C for a time of 25 hours to 60 days. Thereafter, the crystals are separated from the liquid and recovered. It may be desirable to incorporate the zeolite alkylation catalyst with another material, i.e., a binder, which is resistant to the temperatures and other conditions employed in the process of this invention. Suitable binder materials include active and inactive materials and synthetic or naturally occurring zeolite as well as inorganic materials such as clays, silica and/or metal oxides such as alumina. The latter can be either naturally occurring or provided in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. Use of a binder material in conjunction with the 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 also serve as diluents to control the amount of conversion so that products can be obtained economically and in a controlled fashion without having to employ other means for controlling the rate of reaction. These materials can be incorporated into naturally occurring clays, e.g., bentonite and kaolin, to improve the crush strength of the zeolite under commercial operating conditions. Good crush strength is an advantageous attribute for commercial use since it prevents or delays breaking down of the catalyst into powder-like materials. Naturally occurring clays which can be composited with the zeolite crystals include the montmorillonite and kaolin family, which families include the subbentonites, and the kaolines 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 the zeolite also include inorganic oxides, notably alumina. Apart from or in addition to the foregoing binder materials, the zeolite crystals can be composited with an organic oxide matrix 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, silica-magnesia-zirconia, etc. 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 the zeolite and inorganic oxide matrix can vary widely with the zeolite content ranging from 1 to 95 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 alkylation catalyst may be increased by steaming, with suitable stabilization conditions including contacting the catalyst with, for example, 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. Alkylation of the alkylaromatic, e.g. toluene, in accordance with the first step of the process of the invention is effected by contact of the reactants at a temperature of -20 to 480°C (0 to 900°F), preferably 10 to 260°C (50 to 500°F), and a pressure of 20 to 25250 kPa (0.2 to 250 atmospheres), preferably 100 to 2525 kPa (1 to 25 atmospheres). The molar ratio of alkylaromatic, e.g. toluene, to olefin alkylating agent, e.g. 1-pentene, can be from 0.1:1 to 50:1, preferably from 0.5:1 to 5:1. Reaction is suitably accomplished utilizing a feed weight hourly space velocity (WHSV) of from 0.1 to 500 hr⁻¹, preferably from 0.5 to 100 hr⁻¹. The WHSV is based upon the total weight of active catalyst (and binder if present). The alkylation process step of this invention can be carried out as a batch-type, semi-continuous or continuous operation utilizing a fixed, fluidized or moving bed catalyst system. The product of the alkylation reaction of toluene with 1-pentene contains over 90% isoamyltoluene and is then contacted with a dehydrocyclization catalyst, such as Pt/Ba/K/zeolite L. Zeolite L is a large pore zeolite. The barium and potassium components of the catalyst increase its selectivity for dehydrocyclization reactions. More information regarding use of zeolite L in dehydrocyclization reactions may be found in U.S. Patent No. 4,650,565 and U.S. Patent No. 4,746,764. The dehydrocyclization is conveniently effected at a temperature of 260 to 815°C (500 to 1500°F), a pressure of 100 to 7000 kPa (0 to 1000 psig), and a liquid hourly space velocity (LHSV) of about 0.1 to 20 hr⁻¹. Hydrogen may be employed as a diluent and may be circulated at a rate of from about 1 to 10 moles of hydrogen per mole of charge stock hydrocarbon. Effluent from the dehydrocyclization reaction contains dimethylnaphthalenes including the 2,6 isomer and other isomers, as well as naphthalene and monomethylnaphthalenes. The dimethylnaphthalene fraction may be directed to an isomerization reactor to enhance the concentration of the 2,6 isomer. A process for isomerization of dimethylnaphthalenes employing mordenite type zeolite catalyst is described in U.S. Patent No. 4,777,312. Specifically, the isomerization catalyst described therein comprises mordenite in the hydrogen form dispersed in an alumina matrix and with a Group VIII noble metal (e.g. platinum, palladium, etc.) incorporated therein. The isomerization conditions include a temperature of 300 to 450°C, a pressure of 100 to 2000 kPa (1 to 20 atmospheres), a liquid hourly space velocity of 0.5 to 5 hr⁻¹, and a hydrogen to hydrocarbon molar feed ratio of 1 to 7. Other products from the dehydrocyclization reaction, such as naphthalene and mono-methylnaphthalene, may be directed to an additional alkylation unit where they may be reacted with methanol (CH₃OH) in the presence of the catalyst, and under the conditions, employed in the first alkylation stage. In order to more fully illustrate the process of this invention and the manner of practicing same, the following examples are presented. In examples illustrative of the synthesis of zeolite, 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 follows: 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) cyclohexane vapor, pressure less than the vapor-liquid equilibrium pressure of the respective adsorbate at 90°C. The pressure was kept constant (within about ± 0.5 mm Hg) by addition of adsorbate vapor controlled by a manostat during the adsorption period, which did not exceed about 8 hours. As adsorbate was adsorbed by the crystalline material, 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 adsorbant. Zeolite MCM-22 always exhibits Equilibrium Adsorption values of greater than about 10 wt.% for water vapor, greater than about 4.5 wt.%, usually greater than about 7 wt.% for cyclohexane vapor and greater than about 10 wt.% for n-hexane vapor. These vapor sorption capacities are a notable distinguishing feature of zeolite MCM-22. 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 the highly active silica-alumina cracking catalyst taken as an Alpha of I (Rate Constant = 0.016 sec⁻¹). The Alpha Test is described in U.S. Patent 3,354,078; in the Journal of Catalysis , vol. 4, p. 527 (1965); vol. 6, p. 278 (1966); and vol. 61, p. 395 (1980). The experimental conditions of the test used herein include a constant temperature of 538 o C and a variable flow rate as described in detail in the Journal of Catalysis , vol. 61, p. 395. EXAMPLE 1 One part sodium aluminate (43.5% Al₂O₃, 32.2% Na₂O, 25.6% H₂O) was dissolved in a solution containing 1 part of 50% NaOH solution and 103.13 parts H₂O. To this was added 4.50 parts hexamethyleneimine. The resulting solution was added to 8.55 parts of Ultrasil, a precipitated, spray-dried silica (90% SiO₂). The reaction mixture had the following composition, in molar ratios: SiO₂/Al₂O₃ = 30.0 OH⁻/SiO₂ = 0.18 H₂O/SiO₂ = 44.9 Na/SiO₂ = 0.18 R/SiO₂ = 0.35 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 E. The sorption capacities of the calcined material were measured to be: H₂O 15.2 wt.% Cyclohexane 14.6 wt.% n-Hexane 16.7 wt.% The surface area of the zeolite was measured to be 494 m₂/g. The chemical composition of the uncalcined material was determined to be as follows: Component wt.% SiO₂ 66.9 Al₂O₃ 5.40 Na 0.03 N 2.27 Ash 76.3 SiO₂O/Al₂O₃, mole ratio 21.10 Degrees 2-Theta Interplanar d-Spacing (A) I/I o 2.80 31.55 25 4.02 21.98 10 7.10 12.45 96 7.95 11.12 47 10.00 8.85 51 12.90 6.86 11 14.34 6.18 42 14.72 6.02 15 15.90 5.57 20 17.81 4.98 5 20.20 4.40 20 20.91 4.25 5 21.59 4.12 20 21.92 4.06 13 22.67 3.92 30 23.70 3.75 13 24.97 3.57 15 25.01 3.56 20 26.00 3.43 100 26.69 3.31 14 27.75 3.21 15 28.52 3.13 10 29.01 3.08 5 29.71 3.01 5 31.61 2.830 5 32.21 2.779 5 33.35 2.687 5 34.61 2.592 5 EXAMPLE 2 A portion of the calcined MCM-22 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 F. 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 respectively in stainless steel autoclaves at autogenous pressure. Solids were separated from any unreacted components by filtration and then water washed, followed by drying at 120°C. The product crystals were subjected to X-ray diffraction, which showed the products to be MCM-22. Sorption, surface area and chemical analyses were also carried out and the results are presented in Table F. The sorption and surface area measurements were of the calcined product. Example 3 4 5 Reaction Mixture (mole ratios) SiO₂/Al₂O₃ 30.0 30.0 30.0 OH⁻/SiO₂ 0.18 0.18 0.18 H₂O/SiO₂ 19.4 19.4 44.9 Na/SiO₂ 0.18 0.18 0.18 R/SiO₂ 0.35 0.35 0.35 Product Composition, Wt.% SiO₂ 64.3 68.5 74.5 Al₂O₃ 4.85 5.58 4.87 Na 0.08 0.05 0.01 N 2.40 2.33 2.12 Ash 77.1 77.3 78.2 SiO₂/Al₂O₃ (mole ratio) 22.5 20.9 26.0 Adsorption, Wt.% H₂O 14.9 13.6 14.6 Cyclohexane 12.5 12.2 13.6 n-Hexane 14.6 16.2 19.0 Surface Area, m²/g 481 492 487 EXAMPLE 6 Quantities of the calcined (538°C for 3 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. EXAMPLE 7 To demonstrate a further preparation of the zeolite MCM-22, 4.49 parts of hexamethyleneimine was added to a solution containing 1 part of sodium aluminate, 1 part of 50% NaOH solution and 44.19 parts of H₂O. To the combined solution was added 8.54 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. Product chemical composition, surface area and adsorption analyses results were as set forth in Table G. Surface area and adsorption analyses were on calinced product (538°C). Product Composition (uncalcined) C 12.1 wt.% N 1.98 wt.% Na 640 ppm Al₂O₃ 5.0 wt.% SiO₂ 74.9 wt.% SiO₂/Al₂O₃, mole ratio 25.4 Adsorption, wt.% Cyclohexane 9.1 N-Hexane 14.9 H₂O 16.8 Surface Area, m²/g 479 EXAMPLE 8 This example illustrates the preparation of the zeolite MCM-22 where X in the general formula, supra , is boron. Boric acid, 2.59 parts, was added to a solution containing 1 part of 45% KOH solution and 42.96 parts H₂O. 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. The reaction mixture had the following composition in molar ratios: SiO₂/B₂O₃ = 6.1 OH⁻/SiO₂ = 0.06 H₂O/SiO₂ = 19.0 K/SiO₂ = 0.06 R/SiO₂ = 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 120°C. A portion of the product was calcined for 6 hours at 240°C. and found to have the following sorption capacities: H₂O 11.7 wt.% Cyclohexane 7.5 wt.% n-Hexane 11.4 wt.% The surface area of the calcined crystalline material was measured (BET) to be 405 m²/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.% Al₂O₃ 920 ppm SiO₂ 75.9 wt.% Ash 74.11 wt.% SiO₂/Al₂O₃, molar ratio 1406 SiO₂/(Al+B)₂O₃, molar ratio 25.8 EXAMPLE 9 A portion of the calcined crystalline product of Example 8 was treated with NH₄Cl and again calcined. The final crystalline product was tested in the Alpha test and found to have an Alpha Value of 1. EXAMPLE 10 In another example of the synthesis of the zeolite MCM-22, one part sodium aluminate (43.5% Al₂O₃, 33.3% Na₂O, 24.2% H₂O) dissolved in 0.7 parts water was added to a solution containing 1 part of 50% NaOH solution and 43.5 parts H₂O. Next was added 4.50 parts hexamethyleneimine. Ultrasil, a precipitated, spray-dried silica (90% SiO₂) was next added in the amount of 8.55 parts with stirring. The reaction mixture had the following composition, in molar ratios: SiO₂/Al₂O₃ = 30.0 OH⁻/SiO₂ = 0.18 H₂O/SiO₂ = 19.3 Na/SiO₂ = 0.18 R/SiO₂ = 0.35 where R is hexamethyleneimine. The mixture was crystallized in a stainless steel reactor, with stirring, at 143°C for 3 days. The crystalline product was filtered, washed with water and dried at 120°C. A portion was calcined in N₂ at 538°C for three hours, exchanged twice with ammonium nitrate (5 vol. 1.ON NH₄NO₃/vol cat.), washed nitrate free with deionized water, dried for 16 hours at 120°C and air calcined for 3 hours at 538°C. The X-ray diffraction pattern contained the major lines listed in Tables A-D. EXAMPLE 11 As a first step to the present process, alkylation of 600 grams of a mixture of two parts toluene/one part 1-pentene was carried out in a one liter stirred autoclave using 10.0 grams of the zeolite MCM-22 produced in Example 10. The autoclave was heated to 150°C (300°F) and held at this temperature for 18 hours. The autoclave was then cooled to room temperature and the product analyzed by gas chromatography and mass spectrometry. The analyses showed that the alkylation of toluene was complete and resulted in the selective alkylation of toluene to an alkylate product containing over 90% isoamyltoluene. The autoclave product was distilled to remove the unreacted components. EXAMPLE 12 A dehydrocyclization catalyst for use in the second step of the process was prepared in accordance with the following procedure: Commercial zeolite L was calcined for 3 hours at 540°C (1000°F) in 3 vol/vol/minute nitrogen gas. The zeolite was then exchanged with barium ions (Ba⁺²) for 3 hours at 80°C (176°F) and pH of 10. The zeolite was then filtered, washed, and dried at 120°C (250°F) overnight. The zeolite was then calcined for 3 hours at 540°C (1000°F) in 3 vol/vol/min air. The above steps-were repeated, and the zeolite was then impregnated with a 0.075 M solution of Pt (NH₃)₄Cl₂ using rotary-evaporator/incipient wetness techniques under a carbon dioxide atmosphere. The zeolite was then rolled for one hour under carbon dioxide atmosphere, dried, and then heated at 1°C (2°F)/minute to 260°C (500°F), and calcined for 2 hours at 260°C (500°F) in 5 vol/vol/minute of air. The resulting crystalline product was a Pt/Ba/K/Zeolite L containing 0.87 wt.% platinum. EXAMPLE 13 As the second step of the present process, the isoamyltoluene-containing product from Example 11 was reacted under dehydrocyclization conditions with the Pt/Ba/K/zeolite L catalyst produced in Example 12. The dehydrocyclization reaction was performed in a fixed bed pilot unit equipped with a downflow 1.3 cm (1/2 inch) ID stainless steel reactor. The top portion of the reactor was packed with 5 cc of commercially available sulfur guard (HRD-264), and the lower portion was packed with 10 cc of the Pt/Ba/K/zeolite L. The sulfur guard was pretreated in hydrogen at 260°C (500°C) for 4 hours prior to loading. The catalyst bed was heated at a rate of 105°C (220°F)/hour in 100 cc/min of flowing hydrogen to 485°C (905°F), and then held at this temperature for one hour. Performance of the dehydrocyclization catalyst was initially tested with a n-hexane feed at 485°C (905°F), 790 kPa (100 psig), 3 WHSV, and 3:1 H₂/HC. The observed aromatics selectivity and C₆ paraffin conversion (Table H) were comparable to values reported in the patent literature. After catalyst performance was confirmed, the n-hexane feed was removed and replaced with the alkylate product from Example 11 (>90% isoamyltoluene). Liquid and gaseous products from the reaction were collected and analyzed on a non-polar capillary column. The data are given in Table H. Selectivities for naphthalenes and dimethyl-naphthalenes were 15.6% and 5.6%, respectively. The data given in Table H show that the process disclosed herein can generate dimethylnaphthalenes directly from low cost starting materials. Dehydrocyclization of Alkylates Test Run Process Step Feed n-hexane Ex. 16 Product WHSV (hr⁻¹) 3.2 1.1 Product Distribution, wt.% C₅- 19.8 45.3 Total Aromatics 36.3 54.3 Naphthalenes (Naph) 0 8.4 Dimethylnaphthalenes (DMN) 2.7 Aromatics Selectivity 64.7 54.5 Naph Selectivity 0 15.6 DMN Selectivity 0 5.6

Claims: A process for producing dimethylnaphthalene from a feedstock containing toluene and a C₅ olefin, said process comprising the steps of: a) contacting said feedstock with an alkylation catalyst composition to produce an alkylate, said catalyst composition comprising a synthetic crystalline zeolite having a Constraint Index of not greater than 5, and b) contacting said alkylate with a dehydrocyclization catalyst to produce a product containing dimethylnaphthalene. The process of Claim 1 wherein said crystalline zeolite of said alkylation catalyst composition has a Constraint Index of not greater than about 3. The process of claim 1 wherein the crystalline zeolite is selected from ZSM-4, ZSM-12, ZSM-20, ZSM-35, ZSM-48, ZSM-50, MCM-22, TMA offretite, mordenite, clinoptilolite, zeolite Y and zeolite Beta. The process of claim 1 wherein the crystalline zeolite has, in its calcined form, an X-ray diffraction pattern including interplanar d-spacings as set forth in Table A below. Interplanar d-Spacing (A) Relative Intensity, I/I o x 100 12.36 ± 0.4 M-VS 11.03 ± 0.2 M-S 8.83 ± 0.14 M-VS 6.18 ± 0.12 M-VS 6.00 ± 0.10 M-M 4.06 ± 0.07 W-S 3.91 ± 0.07 M-VS 3.42 ± 0.06 VS The process of any preceding Claim wherein the C₅ olefin is 1-pentene. The process of any preceding Claim wherein the alkylation conditions include a temperature of -20 to 480°C (0 to 900°F) and a pressure of 20 to 25250 kPa (0.2 to 250 atmospheres). The process of any preceding Claim wherein the alkylation conditions include a temperature of 10 to 260°C (50 to 500°F) and a pressure of 100 to 2525 kPa (1 to 25 atmospheres). The process of any preceding Claim wherein the dehydrocyclization catalyst comprises zeolite L. The process of any preceding Claim wherein the dehydrocyclization conditions include a temperature of 260 to 815°C (500 to 1500°F) and a pressure of 100 to 7000kPa (0 to 1000 psig).

Inventors: DEL ROSSI KENNETH JOSEPH, GREEN LARRY ARTHUR, HUSS ALBIN JR, KIRKER GARRY WAYNE, LANDIS MICHAEL EUGENE, DEL ROSSI, KENNETH JOSEPH, GREEN, LARRY ARTHUR, HUSS, ALBIN, JR., KIRKER, GARRY WAYNE, LANDIS, MICHAEL EUGENE
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1991
Main classification: C07C15
IPC codes: C07C5, C07C15, B01J29, C07B61, C07C2