ALKYLAROMATIC ISOMERIZATION PROCESS

Abstract: In a process for catalytically converting feedstock alkylaromatic compounds having 8 to 50 carbon atoms to product aromatic compounds which differ from said feedstock aromatic compounds, the feedstock is contacted with a catalyst composition comprising the synthetic porous crystalline zeolite MCM-22.

Description: ALKYLAROMATIC ISOMERIZATION PROCESS This invention relates to a process for converting a feedstock comprising alkylaromatic compounds of from 8 to 50 carbon atoms, e.g. monocyclic alkyl-substituted benzene of from 8 to 30 carbon atoms, polycyclic, e.g. polyphenyl, compounds of from 12 to 50 carbon atoms, and mixtures thereof, to a product comprising aromatic compounds which differ from those of said feedstock. U.S. Patent 4,380,685 teaches para-selective alkylation, transalkylation or disproportionation of a substituted aromatic compound to form a dialkylbenzene compound mixture over catalyst comprising zeolite characterized by a constraint index of 1 to 12 and a silicaϊalumina mole ratio of at least 12:1, the catalyst having thereon incorporated various metals and phosphorus. Other patents covering alkylation and transalkylation include U.S. Patents 4,127,616, 4,361,713, 4,365,104, 4,367,359, 4,370,508 and 4,384,155. Toluene is converted to para-xylene in U.S. Patents 3,965,207, 3,965,208, 3,965,209, 4,001,346, 4,002,698, 4,067,920, 4,100,215 and 4,152,364. Alkylation with olefins is taught, for example, in U.S. Patents 3,962,364 and 4,016,218 and toluene is disproportionated in, for example, U.S. Patent 4,052,476, 4,007,231, 4,011,276, 4,016,219 and 4,029,716. Isomerization of xylenes is taught in, for example, U.S. Patents 3,856,871; 3,856,872; Re. 30,157; 4,100,214; 4,101,595; 4,101,596; 4,101,597; 4,152,363; 4,158,676; 4,159,282; 4,159,283; Re. 31,782; 4,163,028; 4,188,282; 4,224,141; 4,385,195; and 4,351,979. U.S. Patent 4,826,667 shows isomerization of xylenes over catalyst comprising SSZ-25. Octafining for ^ manufacture of p-xylene is referred to in "Advances in "Petroleum Chemistry and Refining", Vol. 4, p. 433, 1961 (Interscience Publishers, NY) . The present invention resides in a ' process for catalytically converting feedstock alkylaromatic 5 compounds having 8 to 50 carbon atoms to product aromatic compounds which differ from said feedstock aromatic compounds, the process comprising contacting said feedstock with a catalyst composition comprising a synthetic porous crystalline zeolite having an X-ray ■10 diffraction pattern as set forth in Table I of the specification. The process of the invention employs a catalyst comprising a synthetic, thermally stable, crystalline zeolite referred to herein as MCM-22. In its calcined J.5 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 Table I below: TABLE I 20 Interplanar d-Spacinσ (A) Relative Intensity. I/Io x 100 30.0 ± 2.2 -M 22.1 ± 1.3 12.36 ± 0.4 M-VS 11.03 ± 0.2 M-S 25 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 30 3.42 ± 0.06 VS or more specifically an X-ray diffraction pattern including the following lines: TABLE II Interplanar d-Spacin (A) Relative intensity, I/Io 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 These values were determined by standard techniques. 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 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 -1° in terms of the symbols W=weak, M=medium, S=strong and VS=very strong. In terms of intensities, these may be generally designated as follows: W = 0 - 20 M = 20 - 40 -15 S = 40 - 60 VS = 60 - 100 Zeolite MCM-22 has a composition involving the molar relationship: X 2 0 3 :(n)Y0 2 , 20 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 25 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 0 2 , as follows: (0.005-0.l)Na 2 0: (l-4)R:X 2 0 3 :nY0 2 30 wherein R is an organic, normally hexamethylenei ine. The R and Na components are associated with the zeolite as a result of their presence during crystallization, and are easily removed by conventional post-crystallization methods. 35 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, an organic (R) directing agent, e.g. hexamethyleneimine, and water, said reaction mixture having a composition, in terms of mole ratios of oxides, within the following ranges: MCM-22, the Y0 2 reactant contains a substantial amount of solid Y0 2 , e.g. at least 30 wt.% solid Y0_. Where Y0 2 is silica, the use of a silica source containing at least 30 wt.% solid silica, e.g. Ultrasil (a precipitated, spray dried silica containing about 90 wt.% silica) or HiSil (a precipitated hydrated SiO containing about 87 wt.% silica, about 6 wt.% free H O and about 4.5 wt.% bound H,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 SiO 8.9 wt.% Na 0 and 62.3 wt.% H 2 0) is used, crystallization may yield little, if any, MCM-22 crystalline material and impurity phases of other crystal structures, e.g. ZSM-12, may be produced. Preferably, therefore, the Y0 2 , e.g. silica, source contains at least 30 wt.% solid YO_, e.g. silica, and more preferably at least 40 wt.% solid YO_, e.g. silica. Crystallization of the MCM-22 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 t a temperature of 80°C to 225°C for a time of 25 hours to 60 days. Thereafter, the crystals are separated from the liquid and recovered. Synthesis of the MCM-22 is facilitated by the presence of at least 0.01%, preferably at least 0.10% and still more preferably at least 1%, seed crystals based on the total weight of the crystalline product formed. It can be advantageous to composite the zeolite MCM-22 with other materials, i.e. a matrix or binder, 0 which are resistant to the temperature and other conditions employed in the present process. Useful matrix materials include both synthetic and naturally-occurring substances, e.g. inorganic materials such as clay, silica and/or metal oxides. 5 Such materials can be either naturally-occurring or can be obtained as gelatinous precipitates or gels including mixtures of silica and metal oxides. Naturally-occurring clays which can be composited with MCM-22 include those of the montmorillonite and kaolin 2o families, which families include the sub-bentonites and the kaolines commonly known as Dixie, McNamee, Georgia and Florida clays or others in which the main mineral constituent is haloysite, kaolinite, dickite, nacrite or anauxite. Such clays can be used in the raw state 25 as originally mined or initially subjected to calcination, acid treatment or chemical modification. In addition to the foregoing materials, the zeolite catalyst can be composited with a porous metal oxide binder material such as alumina, titania, ■30 zirconia, silica, silica-alumina, silica-magnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania, etc., as well as ternary oxides compositions such as silica-alumina-thoria, silica-alumina-zirconia, silica-alumina-magnesia, 35 silica-magnesia-zirconia, etc. The binder juaterial can be in the form of a cogel. It may be advantageous to provide at least part of the binder, e.g. an amount representing from 1 to 100 weight percent and preferably from 2 to 60 weight percent of the total binder material, in colloidal form so as to facilitate the extrusion of the zeolite bound therewith. Since MCM-22 is synthesized nearly free of alkali metal ions, it can be used in the process of this invention without ion-exchange. To the extent desired, however, the original alkali metal ions, e.g. sodium, 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 ions. Preferred replacing ions include metal ions, hydrogen ions, hydrogen precursor, e.g. ammonium, ions and mixtures thereof. Particularly preferred ions are those which tailor the catalytic activity for certain hydrocarbon conversion reactions. 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 synthetic porous crystalline MCM-22 present in the catalyst composition herein can also be used in intimate combination with a hydrogenating component such as tungsten, vanadium, molybdenum, rhenium, nickel, cobalt, chromium, manganese, or a noble metal such as platinum or palladium where a hydrogenation- dehydrogenation function is to be performed. Such component can be associated chemically and/or physically with the MCM-22 and/or matrix with which the MCM-22 may be optionally composited. Thus, for example, the hydrogenating component can be introduced into the catalyst composition by way of co-crystalli¬ zation, exchanged into the composition to the extent a Group IIIA element, e.g. aluminum, is in the structure, impregnated therein or intimately physically admixed therewith. Such component can be impregnated in, or on, the synthetic porous crystalline material such as, for example, by, in the case of platinum, treating the synthetic porous crystalline material with a solution containing the platinum metal-containing ion. Thus, suitable platinum compounds for this purpose include chloroplatinic acid, platinous chloride and various compounds containing the platinum amine complex. The stability of the zeolite catalyst may be increased by steaming, with suitable steam 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. Feedstock aromatic compounds which can be isomerized according to the process of the invention include alkylaromatic compounds having 8 to 50 carbon atoms, such as monocyclic alkyl-substituted benzenes of from 8 to 30 carbon atoms having the structure wherein R* is a C to C.- alkyl, methyl, ethyl, propyl or a combination thereof, and n is an integer of from 2 to 4. In other words, the feedstock aromatic compounds may be benzene containing from 2 to 4 methyl, ethyl and/or propyl group substituents, and mixtures thereof. Non-limiting examples of such feedstock compounds include xylene, diethylbenzene, diisopropylbenzene, mesitylene (1,3,5-trimethylbenzene) , durene (1,2,4,5-tetra-methylbenzene) , pseudocumene (l,2,4-trimethylbenzene) and mixtures thereof. Polycyclic, e.g. polyphenyl, aromatic compounds having 12 to 50 carbon atoms, such as, alkylbiphenyl, alkyldiphenylmethane, alkylnaphthalene, alkylanthracene and alkylstilbene, can also be isomerized aβcording to the invention. In general, the present process is conducted at a temperature of 40 to 540°C (100 to 1000°F), a pressure of from 100 to 7000 kPa (0 to 1000 psig) " , a weight hourly space velocity of from about 0.1 hr to about 5 50 hr and a hydrogen/feedstock hydrocarbon compound mole ratio of from 0 (no added hydrogen) to 10. Preferred processes according to the invention include isomerization of a xylene-containing feedstock to a product enriched in p-xylene and isomerization of -10 trimethylbenzene and/or ethyltoluene. With such processes, the preferred reaction conditions including a temperature of 120 to 510°C (250 to 950 β F), preferably 200 to 480°C (400 to 900°F) , a pressure of 270 to 5270 kPa (25 to 750 psig) , preferably 450 to 5 3550 kPa (50 to 500 kPa) , a weight hourly space velocity of 0.5 to 35 hr~ , preferably 1 to 25 hr~ , and a hydrogen/hydrocarbon mole ratio of 0.1 to 7.5, preferably 0.5 to 5. In order to more fully illustrate the process of 0 this invention and the manner of practicing same, the following examples are presented. In the examples, whenever sorption capacities for water, cyclohexane and/or n-hexane are given, they are Equilibrium Adsorption values determined as follows: 5 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 0 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 Hg) by addition of adsorbate vapor controlled by a manostat during the adsorption period, which did not 5 exceed about 8 hours. As adsorbate was adsorbed by the MCM-22 crystalline material, the decrease ift 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 5 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 -10 and greater than about 10 wt.% for n-hexane vapor. 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 15 constant (rate of normal hexane conversion per volume of catalyst per unit time) . It is based on the activity of silica-alumina cracking catalyst taken as an Alpha of 1 (Rate Constant = 0.016 sec " ). The Alpha Test is described in U.S. Patent 3,354,078; in the 20 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°C and a variable flow rate as described in detail in the Journal of 25 Catalysis, vol. 61, p. 395. EXAMPLE 1 A mixture of sodium aluminate (43.5% A1_0 3 , 32.2% Na 0, 25.6% H-0) , water, sodium hydroxide, hexamethyleneimine and Ultrasil, a precipitated, 30 spray-dried silica (about 90% SiO_) , having the composition, in mole ratios, given in Table III was prepared. The mixture was maintained at 143"C for 8 days, in a stainless steel, stirred (350 rpm) autoclave at autogenous pressure. Solids were separated from any - 35 unreacted components by filtration 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 and the results are presented in Table III. The sorption and surface area measurements were of the calcined product. TABLE III A quantity of the calcined (540°C for 3 hours) the resultant MCM-22 product was tested in the Alpha Test and found to have an Alpha Value of 180. EXAMPLE 2 In a glass reactor, a catalyst composed of a 0.2 gram sample of the product of Example 1, calcined in air for 3 hours, was heated to 260 0 C (500°F). A mixture of 1,3,5-triethylbenzene and benzene in 10/90 weight ratio was charged into the reactor at the rate of 2 ml/hour together with nitrogen carrier gas. Reaction conditions were maintained at 260%C (500°F) , atmospheric pressure and 10 hr WHSV. The * 1,3,5-triethylbenzene was in part isomerized to 1,2,4-triethylbenzene with conversion by isomerization measured to be 23%. EXAMPLE 3 A further sample of zeolite MCM-22 was prepared by adding 4.49 parts quantity of hexamethyleneimine to a mixture containing 1.00 part sodium aluminate, 1.00 part 50% NaOH, 8.54 parts Ultrasil VN3 and about 44.19 parts deionized H_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. The product zeolite was then calcined in nitrogen at 540°C, exchanged with aqueous ammonium nitrate and calcined in air at 540"C. The zeolite was tabletted, crushed and sized to 30/40 mesh. It had the following properties: Surface Area (BET) , m 2 /g 503 Si0 2 /Al 2 0 3 (molar) 27 Na, ppm 495 Sorption Properties, wt.% H 2 0 15.0 cyCo. 12.5 Ash at 1000°C, wt.% 99.05 EXAMPLE 4 Portions of catalyst prepared in Example 3 were loaded into glass reactors and heated to 260°C (500°F) . Liquid feedstock composed of 1, 2,3-trimethylbenzene (TMB) alone, and a 50/50 wt. mixture of 1,2,3-TMB and benzene were pumped into the reactors to prβvide a WHSV of 2 hr " . After 30 minutes on line, samples of the products provided the results listed in Table IV showing isomerization of the 1,2,3-TMB. TABLE IV Test Conditions Products Dist., wt. C 6 " 0.21 Benzene 47.86 Toluene 0.42 4.26 p-, m-Xylene 2.16 1.33 o-Xylene 1.27 0.93 1,3,5-TMB 20.27 12.33 1,2,4-TMB 59.37 27.11 1,2,3-TMB 9.32 3.12 EXAMPLE 5 A portion of the MCM-22 catalyst prepared in Example 3 was placed in the glass reactor and contacted with o-xylene feed at 260°C, atmospheric pressure and -1 10 hr WHSV. A product sample after 30 minutes on stream proved to comprise the following components (wt.%) : Toluene 0.78 p-Xylene 7.72 m-Xylene 26.26 o-xylene 64.62 0.61 C 9 + EXAMPLE 6 A catalyst comprising 65% MCM-22 prepared as in Example 3 and 35% alumina binder was contacted with m-xylene feed at 315°C (600"F), atmospheric pressure and a WHSV of 3.4 hr ~ . Helium carrier gas was used at 2.1 moles He per mole of hydrocarbon. After 20 minutes on stream a sample of the product proved to comprise the following components (wt.%): Benzene 0.02 Toluene 1.95 m + p-Xylene 77.46 o-Xylene 18.93 C α Aromatics 1.38 C + Aromatics 0.12 Selectivities for the process of this example were as follows (wt.%): (m + p)/(m + p + o) -Xylenes 80.36 o/ (m + p + o) -Xylenes 19.64 o-Xylenes made/conv. 83.96 Aromatics (non-C β )/o-Xylenes 18.40 EXAMPLE 7 In a further synthesis of 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 about 44.19 parts of H_0. 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 (uncalcined) , surface area and adsorption analyses results are set forth in Table V: TABLE V 12.1 wt.% 1.98 wt.% 640 ppm 5.0 wt.% SiO„ 74.9 Wt.% SiO /A1 2 0 , mole ratio 25.4 Adsorption, wt.% 10 Cyclohexane 9.1 n-Hexane 14.9 H 2 0 16.8 Surface Area, m /g 479 EXAMPLE 8 15 A sample of MCM-22 prepared as in Example 7 was combined with alumina to form a mixture of 65 parts by weight zeolite and 35 parts A1 2 0 3> Water was added to this mixture to allow the resulting catalyst to be formed into extrudates. The catalyst was activated by 20 calcining in nitrogen at 540"c (1000°F) , followed by aqueous ammonium nitrate exchange and calcining in air at 540dc (1000 β F) . The resulting catalyst was then treated for 24 hours at 620 β C (1150°F) in 100% steam. Platinum was incorporated into a portion of the steamed catalyst by adding an aqueous solution of Pt(NH ) Cl under partial vacuum. After the addition of the platinum solution was completed, the catalyst sample was mixed for 1 hour in a CO atmosphere. After drying in air for 4 hours at room temperature and 16 hours at 30 115 ° C (240°F) , the catalyst was calcined in 5v/v/min. air at 350°C (660°F) for 3 hours. It contained 0.97% Pt. EXAMPLE 9 A portion of the catalyst prepared in Example 8 _ * was sized and charged to a reactor and the feed described in Table VI was introduced at reaction conditions of 420°C (790°F), 1480 kPa (200 psig), 10.0 hr ""1 WHSV and 2.5:1 H 2 /HC molar ratio. -After 12 hours the reaction product was analyzed. Table VII summarizes the results of the product analysis. Ethylbenzene conversion proved to be 32.80%, xylene loss was only 11.44% and approach to p-xylene equilibrium was 101.1%. Table VI EXAMPLE 10 A sample of MCM-22 prepared as in Example 7 was combined with alumina to form a mixture-of 65 parts by weight zeolite and 35 parts Al^O.,. Water was added to this mixture to allow the resulting catalyst to be formed into extrudates. The catalyst was activated by calcining in nitrogen at 540°C (1000°F), followed by aqueous ammonium nitrate exchange and calcining in air at 540°c (lOOO'F) . EXAMPLE 11 A portion of the catalyst prepared in Example 10 was sized to 14/24 mesh and charged to a glass reactor. The reactor was preheated to 315°C (600 β F) and the feed described in Table VIII was introduced at reactor conditions of 5 hr WHSV, 100 kPa (0 psig) and 100 cc/min N_. After 1 hour on stream, liquid product was collected and analyzed. The results of this analysis are presented in Table IX. Table VIII Feed Component Wt.% p-Ethyltoluene 1.47 m-Ethyltoluene 1.56 o-Ethyltoluene 27.75 1,2,4-Trimethylbenzene 8.32 1,3,5-Trimethylbenzene 60.89 Table IX Product Component Wt.% p-Ethyltoluene 6.29 m-Ethyltoluene 3.35 o-Ethyltoluene 14.10 1,2,3-Trimethylbenzene 5.25 1,2,4-Trimethylbenzene 37.47 1,3,5-Trimethylbenzene 27.25 Conversion/Selectivity o-Ethyltoluene Conv. 87.9% p-Ethyltoluene Selectivity* 51.4% 1,3,5-Trimethylbenzene Conv. 55.2% 1,2,4-Trimethylbenzene Selectivity ** 86.7% *p-Ethyltoluene Selectivity = (wt.% p-Ethyltoluene Produced)/ (wt.% o-Ethyltoluene Converted) **1,2,4-Trimethylbenzene Selectivity - (wt.% 1,2,4-TMB Produced)/ (wt.% 1,3,5-TMB Converted)

Claims: Claims : 1. A process for catalytically converting feedstock alkylaromatic compounds having 8 to 50 carbon atoms to product aromatic compounds which differ from said feedstock aromatic compounds, the process comprising contacting said feedstock with a catalyst composition comprising a synthetic porous crystalline zeolite having an X-ray diffraction pattern as set forth in Table I of the specification. 2. The process of claim 1 wherein said synthetic porous crystalline zeolite has an X-ray diffraction pattern as set forth in Table II of the specification. 3. The process of claim 1 wherein the zeolite has a composition comprising the molar relationship: X 2 0 3 :(n)Y0 2 wherein X is a trivalent element, Y is a tetravalent element and n is at least 10. 4. The process of claim 3 wherein X is selected from aluminum, boron, iron, gallium and combinations thereof and Y is selected from silicon, germanium and combinations thereof. 5. The process of claim 3 wherein X comprises aluminum and Y comprises silicon. 6. The process of claim 3 wherein n is 10 to 60. 7. The process of claim 1 wherein said contacting is effected at a temperature of 40 to 540 ° C (100°F to 1000 β F), a pressure of 100 to 7000kPa (0 to 1000 psig), a weight hourly space velocity of 0.1 to 50 hr and a hydrogen/feedstock hydrocarbon compound mole ratio of 0 to 10. 8. The process of claim 1 wherein said contacting is effected at a temperature of 200 to 480°C (400 to 900"F), a pressure of 450 to 3550 kPa (50 to 500 kPa) , a weight hourly space velocity of- 1 to 25 hr , and a hydrogen/hydrocarbon mole ratio of 0.5 to 5. 9. The process of claim 8 wherein said feedstock contains xylenes and the product is enriched in p-xylene.

Inventors: CHU POCHEN, KIRKER GARRY WAYNE, KUSHNERICK JOHN DOUGLAS, MARLER DAVID OWEN, CHU, POCHEN, KIRKER, GARRY, WAYNE, KUSHNERICK, JOHN, DOUGLAS, MARLER, DAVID, OWEN
Applicants: MOBIL OIL CORP, MOBIL OIL CORPORATION
Application year: 1991
Main classification: C07C5
IPC codes: B01J29, C07B61, C07C5, C07C15