A PROCESS FOR ISOMERIZING XYLENES

Abstract: A mixture of aromatic hydrocarbons, comprising xylenes, is isomerized in the presence of ZSM-22 zeolite to produce a product stream wherein the proportion of para­ xylene is substantially equal to the equilibrium ratio of the para-isomer. The process is conducted at 500°F to 1100°F (260 to 593°C), at 0 to 3000 psig (101 to 20785 kPa), optionally in the presence of hydrogen, and also optionally with the catalyst comprising 0.005% to 5.0% of a metal, e.g., platinum, palladium or cobalt, based on total catalyst weight.

Description: A FROCESS FOR ISOMERIZING XYLENES This invention relates to a process for isomerizing xylenes. P-xylene is a valuable chemical feedstock which may be separated for use in synthesis of polyesters from mixed xylenes by fractional crystallization. Typically, p-xylene is derived from mixtures of C8 aromatics separated from such raw materials as petroleum naphthas, particularly reformates, usually by selective solvent extraction. The C8 aromatics in such mixtures and their properties are: Freezing Boiling Density lbs/U.S. Point oF (OC) Point OF (00) Gallon/(k/m3) Ethylbenzene -139.0 (-95) 277.0 (136.1) 7.26 (724.38) P-xylene 55.9 (13.3) 281.0 (13s.3) 7.21 (719.39) M-xylene - 54.2 (-31.2) 282.4 (139.1) 7.23 (721.38) O-xylene - 13.3 (-25.2) 292.0 (144.4) 7.37 (735.35) Calculated thermodynamic equiliDria for the C8 aromatics at 850 F (4540C) are: Wt. % ethyl benzene 8.5 Wt. % para xylene 22.0 Wt. % meta xylene 48.0 Wt. % ortho xylene 21.5 TOTAL 100.0 Principal sources of such raw materials are catalytically reformed naphthas and pyrolysis distillates. The C8 aromatic fractions from these sources may vary quite widely in composition, but they usually comprise 10 to 32 wt. % ethylbenzene, with the balance, xylenes, being divided approximately as 50 wt. S of the meta, and 25 wt. %, each of the para and ortho isomers. Individual isomer products may be separated from the naturally occurring mixtures by appropriate physical methods. Ethylbenzene may be separated by fractional distillation, although this is a costly operation. Ortho-xylene may be separated by fractional distillation, and it is so produced commercially. Para-xylene is separated from the mixed isomers by fractional crystallization or by selective adsorption (e.g;, the Parex process). As commercial use of para and ortho xylene has increased, isomerization of the other C8 aromatics to produce an equilierium mixture of xylenes, and tnus increase the yields of the desired xylenes, has beccme ircreasingly important. Octafining is one of the processes which produce an increased amount of xylenes. In a typical plant utilizing the Octafining process, a mixture of C8 aromatics is introduced to an ethylbenzene tower wherein the stream is stripped of a portion of its ethylbenzene content, to an extent consistent with retaining all the xylenes in the feed stream without unduly expensive 'tsuperfractionationl'. Ethylbenzene is taken off as overhead, while a bottom stream, consisting principally of xylenes, together with a significant amount of ethylDenzene, passes to a xylene splitter column. The bottoms stream from the xylene splitter, comprising primarily ortho-xylene (o-xylene) and Cg aromatics, passes to the o-xylene tower from which o-xylene is taken off as overhead, and heavy ends are removed. The overhead from the xylene splitter column is transferred to a conventional crystallization separator which operates in the manner described in U.S. Patent No. 3,662,013. Because its melting point is much higher than that of the other Ca aromatics, para-xylene (p-xylene) is readily separated in the crystallizer after refrigeration of the stream, and a xylene mixture lean in p-xylene is transferred to an isomerization unit. The isomerization charge passes through a heater, is admixed with hydrogen, and the mixture is introduced to the isomerizer. Isomerized product from tne isomerizer is cooled and passed to a high pressure separator from which separated hydrogen can be recycled in the process. The liquid product of the isomerization passes to a stripper from which light ends are passed overhead. The remaining liquid product comprising primarily C8+ hydrocarbons is recycled in the system to the inlet of the xylene splitter. It will be seen that the system is adapted to produce quantities of p-xylene from a mixed C8 aromatic feed containing all of the xylene isomers plus ethylbenzene. The key to efficient operation to accomplish that result is the use of the isomerizer which takes crystallizer effluent lean in p-xylene and converts the other xylene isomers in part to p-xylene for further recovery at the crystallizer. Among the xylene isomerization processes available in the art, Octafining was originally unique in its ability to convert ethyloenzene. Earlier xylene isomerization processes required extremely expensive fractionation to separate ethylbenzene from other C8 aromatic fractions. As set forth in the table of properties above, the boiling point of ethylbenzene is very close to those of p and m-xylene. Complete removal of ethylbenzene from the charge by conventional methods, e.g., distillation, is therefore impractical. The usual expedient for solving the problem involved the use of an ethylbenzene separation column in the isomerizer-separator loop when using catalyst other than those used in Octafining. However, Octafining does not require the use of this expensive auxiliary equipment to prevent build up of ethylbenzene in the loop. This advantageous feature is possible because the Octafining catalyst converts ethylbenzene to xylenes. In Octafining, ethylbenzene reacts through ethyl cyclohexane to dimethyl cyclohexanes, which in turn equilibrate to xylenes. Competing reactions are disproportionation of ethylbenzene to ethane and benzene, and hydrocracking of alkyl cyclohexanes. A significant improvement of the Octafining process arose with the introduction of zeolite catalysts, such as zeolite ZSM-5, combined with a metal, such as platinum, as described in U.S. Patent No. 3,856,872. At temperatures of 700-8000F (371-4270C), ethylbenzene is converted by disproportionation over ZSM-5 type catalyst to benzene and diethylbenzene. At higher temperatures, and in the presence of a ZSM-5 catalyst of reduced activity, ethylbenzene and other single ring aromatics are converted by splitting off side chains of two or more carbon atoms as described in U.S. Patent No. 4,188,282. These developments permit upgrading of Octafining reactors by the substitution of the improved (ZSM-5) catalyst. In the known processes for isomerizing a C8 aromatic fraction containing ethylbenzene, conversion of that compound is constrained by the need to hold conversion of xylenes to other compounds to an acceptable level. Thus, although the technique of U.S. Patent No. 3,856,872 provides significant advantages over Octafining in this respect, operating conditions are still selected to balance the advantages of ethylbenzene conversion against the disadvantages of xylene loss by disproportionation and the like. A further advance in the art is predicated on the discovery that certain combinations of catalyst and operating conditions decouple ethylbenzene conversion from xylene loss in a xylene isomerization reaction, thus permitting the use of C8 fractions, which contain ethylbenzene as the feed without sacrifice of xylenes to conditions which will promote adequate conversion of ethylbenzene. These results are obtained by the use of a ZSM-5 catalyst of substantially reduced acid activity, e.g., by dilution, steaming, very high silica/alumina ratio, base exchange with alkali metal and coking. For example, U.S. Patent No. 4,163,028 discloses xylene isomerization and ethylbenzene conversion at high temperature with the ZSM-5 zeolite of very high silica/alumina ratio, whereby the acid activity of the catalyst is reduced. - At the high temperatures involved, normally 800-1000 F (427-5380C), the zeolite of reduced activity exhibits effective power for isomerization of xylene and for splitting off alkyl side chains of two or more carbon atoms from single ring aromatics at long on-stream periods. The disproportionation activity of the zeolite is severely depressed by the reduced acid activity, resulting in low losses of xylene by that mechanism. That lack of disproportionation activity impairs the capacity of the catalyst to handle trialkyl aromatics of nine or more carbon atoms, e.g., trimethylbenzene, as practiced in some processes. It thus becomes necessary to remove from the recycle stream those components having more than eight carbon atoms to avoid excessive build-up in the system of Cg and higher hydrocarbons. The catalyst also has the capacity to crack paraffins in the charge to lower boiling compounds readily removable from recycle streams by fractionators normally present in the p-xylene recovery/isomerizer loop. By reason of this combination of activities, the catalyst may be used in a system charging reformate without removal of paraffin hydrocarbons, as described in U.S. Patent No. 4,211,836. It has now been found that aromatic feedstocks containing C8 aromatics can be effectively isomerized to produce a higher proportion of para-xylene (p-xylene), than contained in the feedstock, in the presence of ZSM-22 zeolite. The isomerization process may optionally be conducted in the presence of hydrogen, and the catalyst may optionally contain a noble metal component, e.g., platinum. Accordingly, the invention resides in its broadest aspect in a process for isomerizing xylenes from a hydrocarbon mixture to produce a product stream comprising substantially an equilibrium mixture of para-xylene comprising contacting the hydrocarbon mixture with a catalyst comprising a ZSM-22 zeolite having a silica:alumina mole ratio of at least 20 and a Constraint Index of 2.6 at 800OF (4270C), and having the X-ray diffraction pattern of Table I. The present isomerization process may also selectively dealkylate single ring aromatic compounds to remove alkyl side chains of two or more carbon atoms. The ZSM-22 zeolite catalyst has a silica/alumina mole ratio of at least 20 and a Constraint Index of 2.6 at 8000F (4270C), as discussed below. The ZSM-22 zeolite catalyst may be optionally combined with a hydrogenation metal from Groups VIB or VIII of the Periodic Table, e.g., cobalt, nickel, tungsten, rhodium, molybdenum, platinum, palladium or combinations thereof. Preferably, the metal is platinum or palladium. The hydrogenation metal is present in the amount of 0.005% by weight to 5.0% by weight, based on total catalyst weight. The isomerization reactor is maintained at a temperature of 500 to 1100 F (260 to 5930C), preferably 600 to 1000 F (316 to 5380C), and a pressure of O to 3000 psig (101 to 20785 kPa), preferably 50 to 800 psig (4466 to 5617 kPa). In general, it is desirable to operate the process in the presence of hydrogen gas to extend catalyst life and maintain efficiency. The hydrogen to hydrocarbon mole ratio may be from 0.1 to 10, and preferably from 0.5 to 5.0, with a total pressure from 0 up to 3000 psig (101 to 20785 kPa). The space velocity is usually adjusted to provide a desired conversion of ethylbenzene per cycle, usually from 10 to 40S, and with the para isomer content of at least 70%, preferably at least 90% that of equilibrium. The present isomerization process may be incorporated in a reaction train through which a petroleum naphtha is processed for manufacture of p-xylene. Alternatively, the process may be used in a facility utilizing a feedstock of purchased C8 aromatics or mixed xylenes. Typically a light petroleum naphtha is supplied to a catalytic reformer operated to convert napthenes to aromatics by dehydrogenation under hydrogen pressure over a catalyst of platinum supported on alumina. In one embodiment, an aromatic-rich reformate product is fractionated to separate compounds of eight carbon atoms (C8) which are then extracted with a suitable selective solvent to separate aromatics from paraffins and provide a C8 aromatics fraction The C8 aromatics fraction prepared by the solvent extraction stage may be fractionated for removal of some ethylbenzene. The degree of ethylbenzene removal, if practiced1 may be accommodated to the desires of the operator, since the present process can tolerate considerable amounts of ethylbenzene (which is converted to benzene). The C8 aromatic fraction, optionally containing varying amounts of ethylbenzene, is conducted to the high temperature isomerizer, wherein the' isomerization of xylenes to yield increased p-xylene content product takes place. however, the ZSM-22 zeolite catalyst used herein also has the capability to convert paraffins to lower boiling alkanes and alkenes which are readily separable by fractionation, and hence it is possible to charge the entire unextracted C8 fraction of the reformer product to the isomerizer. Thus, if desired, the full range reformate may be charged to the isomerizer containing ZSM-22 zeolite in order to make benzene, toluene and xylenes (BTX) from higher boiling aromatics in the manner and under the conditions descriDed in U.S. Patent No. 4,188,282. In any event, fresh feed to the isomerizer contains the C8 aromatic fraction, optionally containing paraffins, and containing some ethylbenzene. The feed also usually contains the xylenes generated by reforming, along with other aromatics ooiling in the xylene range or higher. Under the high temperature conditions prevailing in the isomerizer, the ZSM-22 catalyst has the capacity (1) to isomerize xylenes, thereby restoring equilibrium concentrations in the mixed xylenes of the feed to generate additional p-xylene, (2) to remove alkyl chains of two or more carbon atoms from single ring aromatics, leaving methyl groups to thereby generate BTX, and (3) to crack normal paraffins to lower boiling compounds which can be removed in the downstream fractionators. The effluent of the reactor contains the three xylenes in proportions approaching the thermodynamic equilibrium value together with conversion products from reaction of ethylbenzene and higher boiling alkyl aromatics, as well as a portion of unreacted ethylbenzene and higher aromatics. The by-products of the reaction include benzene, toluene and xylenes derived by reactions of such compounds as ethylbenzene, methylethylbenzene and dimethylethylbenzene. The reaction mixture is fractionated to take compounds of five or less carbon atoms overhead, to withdraw benzene and toluene as a side stream, and the bottoms stream comprising substantially aromatics of eight or more carbon atoms. The bottoms fraction is then fractionated in a separate fractionator to remove therefrom aromatics of nine or more carbon atoms as bottoms. The overhead fraction of that fractionator, comprising eight carbon atom aromatics is transferred as feed to a p-xylene separator of a conventional design from which a fraction depleted in p-xylene is recycled to the isomerization reactor. The crystalline aluminosilicate (zeolite) ZSM-22 catalyst used herein promotes a reaction course which is unique at temperatures of 500 to 1100 F (260 to 5930C). Ethylbenzene in the charge is selectively cracked to benzene at little or no conversion of xylenes. Two or more carbon atom chains on other aromatics undergo similar conversion. The two types of conversion are decoupled such that reaction severity is not a compromise to achieve effective ethyl aromatic conversion at "acceptable" loss of xylene. This characteristic of the process renders unnecessary the preliminary distillation to separate at least some of the ethylbenzene and Cg+ aromatics from the feed stream, as practiced in prior art processes. The ZSM-22 highly siliceous zeolite used herein can be suitably prepared from a reaction mixture containing a source of silica, an alkane diamine, an alkali metal oxide or an alkaline earth metal oxide, e.g., sodium, potassium, cesium, calcium or strontium, water, and alumina, and having a composition, in terms of mole ratios of oxides, falling within the following ratios: : Reactants Broad Preferred SiO2/Al2O3 = 20 to Co 30 to 1000 H20/SiO2 = 10 to 100 20 to 60 OH /SiO2 = O to 0.3 0.1 to 0.2 - 0 to 2.0 0.1 to 1.0 SiO2 RN/SiO2 = 0.01 to 2.0 0.05 to 1.0 wherein RN is a functional group of C2-C12 alkane diamine of the type Y -(C )n¯N N (abbreviated CnDN), n = 2 to 12, and preferably is 5 to 8, and M is an alkali metal or an alkaline earth metal and maintaining the mixture at crystallization temperature until crystals of the ZSM-22 zeolite are formed. Thereafter, the crystals are separated from the liquid by any conventional means, washed and recovered. Crystallization can be carried out at either static or stirred conditions in a reactor vessel, e.g., a polypropylene jar or teflon lined or stainless steel autoclaves at 800C (176DF) to 210 C (410OF) for 6 hours to 150 days. Thereafter, the crystals are separated from the liquid and recovered. The composition can be prepared utilizing materials which supply the appropriate oxide. Such materials include aluminates, alumina, silicates, sodium silicate, silica hydrosol, silica gel, silicic acid, sodium, potassium or cesium hydroxide, and an alkane diamine. Suitable diamines are, e.g., ethanediamine, propanediamine, butanediamine, pentanediamine, hexanediamine, heptanediamine, octane-diamine, nonanediamine, decanediamine, undecanediamine, duodecanediamine. The reaction mixture can be prepared either batchwise or continuously. Crystal size and crystallization time of the new crystalline material will vary with the nature of the reaction mixture employed and the crystallization conditions. As set forth above, the ZSM-22 zeolite can be prepared at a relatively wide range of SiO2/A1203 ratios of 20 to infinity (#). HDweverss it has been found that larger alkali metal cations, e.g., and Cs+, are preferably used at the SiO2/Al2O3 ratios of 20 to 90 to obtain ZSM-22 crystals substantially free of impurities or other zeolites. The potassium (K+) cation is preferred at such low SiO/A120= ratios because cesium (Cs) appears to decrease the reaction rate. At the SiO2/A1203 ratios of 90 or above, smaller cations, e.g., sodium (Na+) cations, are preferably used to produce substantially 100% crystalline ZSM-22. The highly siliceous ZSM-22 zeolite comprises crystalline, three-dimensional continuous framework siliconcontaining structures or crystals which result when all the oxygen atoms in the tetrahedra are mutually shared between tetrahedral atoms of silicon or aluminum, and which can exist with a network of mostly SiO2, i.e., exclusive of any intracrystalline cations. Similar crystals form building blocks of materials, such as quartz, cristobalite and a long list of zeolite structures, such as ZSM-5, ZSM-ll, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 (described in European Patent Puolication Number 0,015,132), mordenite and perhaps even faujasite. Not all zeolite structures are known to exist at this time in predominantly SiO2-containing compositions so the above class of materials does not presently include some zeolites, such as zeolite A. In the as-synthesized form, the ZSM-22 zeolite has a calculated composition, in terms of moles of oxides, after dehydration, per 100 moles of silica, as follows: (0.02 to lO)RN:(O to 2)M2XnO:(0 to 5)A1203:1006iO2 wherein RN is a functional group of C2-C12 alkane diamine and M is an alkali metal or an alkaline earth metal having a valence n, e.g., Na, K, Cs, Li, Ca or Sr. ZSM-22 can further be identified by its sorptive characteristics and its X-ray diffraction pattern. The original cations of the as-synthesized ZSM-22 may be replaced at least in part by other ions using conventional ion exchange techniques. It may be necessary to precalcine the ZSM-22 zeolite crystals prior to ion exchange. The replacing ions introduced to replace the original alkali, alkaline earth and/or organic cations may be any that are desired so long as they can pass through the channels within the zeolite crystals. Desired replacing ions are those of hydrogen, rare earth metals, metals of Groups Id, IIA, Isis, IIIA, IIDB, IVA, I"B, VIB and VIII of the Periods Table. 4gong the metals, those particularly preferred are rare earth metals, manganese, zinc and those of Group VIII of the Periodic Table. The ZSM-22 zeolite has a definite X-ray diffraction pattern, set forth below in Table I, which distinguishes it from other crystalline materials. TABLE I Most Significant Lines of ZSM-22 Interplanar d-spacinqs (A) Relative IntensitY (I/Io) 10.9 + 0.2 M-VS 8.7 + 0.16 W 6.94 + 0.10 5.40 + 0.08 W 4.58 + 0.07 W 4.36 + 0.07 VS 3.68 + 0.05 VS 3.62 + 0.05 S-VS 3.47 + 0.04 M-S 3.30 + 0.04 W 2.74 + 0.02 W 2.52 + 0.02 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 2x theta, where theta is the Bragg angle, were determined using algorithms on the computer associated with the spectrometer. From these, the relative intensities, 100 I/Io, where Io is the intensity of the strongest line or peak, and d (obs.) the interplanar spacing in A, corresponding to the recorded lines, were determined. In Table I, the relative intensities are given in terms of the symbols vs = very strong, s = strong, m = medium, w = weak, etc. It should be understood that this X-ray diffraction pattern is characteristic of all the species of ZSM-22 zeolite compositions. Ion exchange of the alkali metal cations with other ions results in a zeolite which reveals substantially the same X-ray diffraction pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur, depending on the silica to alumina ratio of the particular sample, as well as its degree of thermal treatment. The ZSM-22 zeolite freely sorbs normal hexane and has a pore dimension greater than 4 Angstroms. In addition, the structure of the zeolite must provide constrained access to larger molecules. It is sometimes possible to judge from a known crystal structure whether such constrained access exists. For example, if the only pore windows in a crystal are formed by 8-membered rings of silicon and aluminum atoms, then access by molecules of larger cross-section than normal hexane is excluded and the zeolite is not of the desired type. Windows of l0-membered rings are preferred, although, in some instances, excessive puckering or pore blockage may render these zeolites ineffective. Twelve-membered rings do not generally appear to offer sufficient constraint to produce the advantageous hydrocarbon conversions, although puckered structures exist, such as TMA offretite, which is a known effective zeolite. Also, such twelve-membered structures can be conceived that may be operative due to pore blockage or other causes. Rather than attempt to judge from crystal structure whether or not a zeolite possesses the necessary constrained access to molecules of larger cross-section than normal paraffins, a simple determination of the "Constraint Index may be used. The meaning of Constraint Index and its method of determination are fully described in, for example, U.S. Patent No. 3,905,915. ZSM-22 has a Constraint Index of 2.6 at 800oF (4270C). Synthetic ZSM-22 zeolites used herein may be in the organic nitrogen-containing and alkali metal-containing form, the alkali metal form or hydrogen form or another univalent or multivalent cationic form. The as-synthesized zeolite may be conveniently converted into the hydrogen, the univalent or multivalent cationic forms by base exchanging the zeolite to remove the sodium cations by such ions as hydrogen (from acids), ammonium, alkylammonium and arylammonium including RNH3, R3-NH+, R2N 4 and R4N+ where R is alkyl or aryl, provided that steric hindrance does not prevent the cations from entering the cage and cavity structure of the ZSM-22 type crystalline zeolite. The hydrogen form of the zeolite is prepared, for example, by base exchanging the sodium form with a suitable ammonium ion, e.g., ammonium chloride or hydroxide, whereby the ammonium ion is substituted for the sodium ion. The composition is then calcined at a temperature of, e.g., 1000 F (538 C), causing evolution of ammonia and retention of the hydrogen proton in the composition. Other replacing cations include cations of the metals of the Periodic Table, particularly metals other than sodium, most preferably metals of Group IIA, e.g., zinc, and Groups IIIA, IVA, IB, IIB, IIIB, IVB, VIB and Group VIII of the Periodic Table, and rare earth metals and manganese. Ion exchange of the zeolite can be accomplished conventionally, e.g., by admixing the zeolite with a solution of a cation to be introduced into the zeolite. Ion exchange with various metallic and non-metallic cations can be carried out according to the procedures described in U.S. Patents 3,140,251, 3,140,252 and 3,140,253. The ZSM-22 zeolite can optionally 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 desired. Such component can be exchanged into the composition, impregnated therein or physically intimately admixed therewith. Such component can be impregnated in or onto the zeolite, for example, in the case of platinum, by treating the zeolite with a solution containing a platinum metal-containing ion. Thus, suitable platinum compounds include chloro-platinic acid, platinous chloride and various compounds containing the platinum tetrammine-platinum complex. Combinations of the aforementioned metals and methods for their introduction can also be used. Synthetic ZSM-22 zeolite, when employed as a catalyst, should be at least partially dehydrated. This can be accomplished by heating the zeolite to a temperature in the range of 2000C to 6000C in an inert atmosphere, such as air or nitrogen for 1 to 48 hours. Simple dehydration of the crystal can also De performed at lower temperatures, such as room temperature, merely by placing the ZSM-22 zeolite type crystal in a vacuum, but a longer time is required to obtain a sufficient degree of dehydration It may also be desired to incorporate the ZSM-22 crystal with another material resistant to the temperatures and other conditions employed in organic conversion processes. Such materials include active and inactive materials and synthetic or naturally occurring zeolites as well as inorganic materials, such as clays, silica and/or metal oxides. The clays, silica and/or metal oxides may be either naturally occurring or in the form of gelatinous precipitates or gels including mixtures of silica and metal oxides. The use of such additional active material in conjunction with the ZSM-22 crystal, i.e., combined therewith, tends to improve the conversion and/or selectivity of the catalyst in certain organic conversion processes. Inactive materials suitably serve as diluents to control the amount of conversion in a given process so that products can be obtained economically and orderly without employing other means for controlling the rate of reaction. These materials may be incorporated into naturally occurring clays, e.g., bentonite and kaolin, to improve the crush strength of the catalyst under commercial operating conditions. Such materials, e.g., clays or oxides, function as binders for the catalyst. It is desirable to provide a catalyst having good crush strength because in commercial use it is desirable to prevent the catalyst from breaking down into powder-like materials. These clay binders are normally employed for the purpose of improving the crush strength of the catalyst.- Naturally occurring clays which can be composited with the ZSM-22 zeolite include the montmorillonite and kaolin family, which families include the subbentonites, and the kaolins commonly known as Dixie, McNamee-Georgia and Florida clays or others in which the main mineral constituent is halloysite, kaolinite, dickite, nacrite, or anauxite. Such clays can be used in the raw state as originally mined or initially subjected to calcination, acid treatment or chemical modification. Binders useful for compositing with the ZSM-22 crystal also include inorganic oxides, e.g., alumina. In addition to the foregoing materials, the ZSM-22 zeolite can be composited with a porous matrix material, such as silica-alumina, silicamagnesia, silica-zirconia, silica-thoria, silica-beryllia, silica-titania, as well as ternary compositions such as silica-alumina-thoria, silicaalumina-zirconia, silica-alumina-magnesia and silica-magnesia-zirconia. The relative proportions of finely divided crystalline material and inorganic oxide gel matrix vary widely, with the crystal content ranging from 1 to 90 % by weight. The ZSM-22 zeolites used herein preferably exhibit relatively low acid acidity. As the acid activity of these zeolites is reduced, the capacity to catalyze disproportionation declines without substantial decline in the capacity to catalyze dealkylation of such compounds as ethylbenzene having side chains of two or more carbon atoms. Therefore, the isomerization reaction may be decoupled from the ethylbenzene conversion which now proceeds by dealkylation in the presence of the low acidity ZSM-22 zeolite. A significant consequence of this-catalytic property is that recycle of toluene and trimethylbenzene to the reactor is generally undesirable because, due to the lack of disproportionation activity, methylbenzenes will not be converted in significant amounts to xylenes. Hence, recycle of these unreactive species would result in an undesirable build-up in the loop of diluent materials. The low acid activity of the catalyst can be obtained in a variety of manners including forming the ZSM-22 zeolite at high silica/alumina ratio above 200, preferably above 500. Very high dilution with an inert matrix is also effective in lowering the acid activity of ZSM-22 zeolite. For example, composites of a more active form of zeolite ZSM-22 with alumina at a ratio of 5 parts of zeolite and 95 parts of the inert matrix provide a suitable low acid activity catalyst. It is considered preferable to steam the ZSM-22 catalyst prior to its use in the present process to control its acid activity. In particular, the unsteamed catalyst, which may be referred to herein as the precursor catalyst, is steamed under relatively mild conditions, such as for one to ten hours with 100% steam at atmospheric pressure and at a temperature of 8000F to 1000if (427 to 5380C) to reduce its acidity to a measured "Alpha" value in the range of 5 to 50. It is to be understood, of course, that the treating conditions may be altered from those recited, such as by using superatmospheric pressure at reduced temperature, the critical parameter being the controlled acidity of the steamed catalyst. The controlled acid activity of the catalyst is conveniently defined by the "Alpha" scale described in an article published in Journal of Catalysis, Vol. VI, pp. 278-287 (1966). In the alpha test, the catalyst is contacted with hexane under prescribed conditions, and the amount of hexane which is cracked is measured. From this measurement is computed the FAlphat value used herein. For purposes of the present invention, however, all measurements of "Alpha" are to be made at 1000 F (5380C), and all references to "Alpha" are to be understood to refer to the value obtained when the hexane cracking is measured at 10000F (5380C). Any combination of the aforementioned methods may be used to lower the acid activity of the ZSM-22 zeolite. In order to more fully illustrate the nature of the invention and the manner of practicing same, the following examples are presented. In the examples which follow, and elsewhere in the specification, whenever adsorption data are set forth for comparison of sorptive capacities for water, cyclohexane and n-hexane, they were determined as follows: A weighed sample of the calcined zeolite was contacted with the desidered pure adsorbate vapor in an adsorption chamber, evacuated to < 1 mm pressure and contacted with water vapor at 12 mm Hg or n-hexane or cyclohexane vapor at 20 mm Hg pressure, pressures less than the vaporliquid equilibrium pressure of the respective adsorbate at room temperature. The pressure was kept constant (within about-+ 0.5 mm) by addition of adsorbate vapor controlled by a manostat during the adsorption period, which did not exceed 8 hours. As adsorbate was adsorbed by the new crystal, the decrease in pressure caused the manostat to open a valve which admitted more adsorbate vapor to the chamber to restore the pressures to the aforementioned control levels. 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 9/100 9 of calcined adsorbent. EXAMPLE A (Catalyst Preparation) Solution A, containing 192.0 g. of silica sol (30% SiO2) and 200.0 9. water, was mixed with stirring with Solution B, containing 6.7 g. A12(S04)3 . 16H20, 15.5 g. KOH, 33.4 g. l-,6-hexanediamine (CN), and 351.2 g. water, directly into a one-liter stainless steel autoclave. The composition of reaction mixture, in mole ratios, was: SiO2/Al203=90; 0/SiO2=40; OH /SiO2=0.20; K+/Si02=0.29; C6DN/SiO2=0.30. The thus formed hydrogen was heated at 1600C with stirring (400 rpm) for 2 days at autogenous pressure. The resultant crystalline product was filtered, washed with water, and dried on a filter funnel at 110 C. X-ray and scanning electron microscopy (SEM) analysis of the product crystals revealed 100% crystalline ZSM-22 with needle-like crystal morphology(0.5 - 1.0 m in length). The crystals had SiO2/A1203 mole ratio of 76 as determined by chemical analysis. A portion of the sample of the zeolite was heated in a tube furnace in flowing nitrogen (150 ml/ml) at a rate of 20C/min to 550OC, whereupon the flowing gas was switched to air. The sample was heated in air at 5500C for 24 hours, then cooled to room temperature. The calcined zeolite was now placed in a cannister and ballmilled for 17 hours. This ballmilling procedure was capable of fracturing the needle-like ZSM-22 crystals to smaller, roughly equidimensional crystals, without loss of x-ray crystallinity. The ballmilled crystals were now NH4 +-exchanged in one molar (1M) NH NO solution twice at 800C, with stirring, for a total of 6 hours, filtered, washed with water, then dried. The material was then mixed with alumina monohydrate in a 65% zeolite, 35% alumina preparation and extruded to produce 1/16 inch cylindrical particles. EXAMPLE B (Catalyst Preparation) Solution A, containing 192.0 g. silica sol (3CDó Si02) and 200.0 g. water, was mixed with stirring with Solution 8, containing 3.4 g. Al2(SO4)3 . 16H20, 5.5 g. NaOH, 33.4 9. 1,6-hexanediamine (C6DN), and 354.1 g. water, directly into a one-liter stainless steel autoclave. The composition of this mixture, in mole ratios, was: SiO2SA1203 = 180; H2O/SiO2 = 40; OH /SiO2 = 0.10; Na /SiO2 = 0.14; CBN/Si02 = 0.30. The hydrogel was heated at 160 C, with stirring at 400 rpm, at autogenous pressure for 3 days. The crystalline product was filtered, washed with water, and dried. X-ray and SEM analysis of the product showed 100% crystalline ZSM-22 crystals with needle-like morphology (1.0 m in length). The SiO2/A1203 mole ratio of the product was 156. 5.2 g. of this product was heated for 10 hours in flowing dry N2 gas. When cooled to 250C, it was saturated with NH gas, followed by ion exchanges for 4, 16 and 4 hours, respectively, with 260 ml. of 2 N NH4NO3. It was then washed at reflux with 260 ml. of water, followed by an air calcination for 10 hours at 6000C. Finally, 0.75 g. of this material, sized to 14-30 mesh, was impregnated with 2 ml. of aqueous solution containing 0.011% of Pt(NH3)4C12. This final product contained 0.013% Pt on HZSM-22. EXAMPLE 1 (Isomerization Process) A synthetic C8 aromatic feed was passed over the catalyst of Example A at 200 psig (1480 kPa), hydrogen:hydrocarbon mole ratio (H2/HC) of 4, and temperatures and weight hourly space velocity (WHSV) of between 850 and 9000F (454 and 4820C), and 5 and 20, respectively. The experimental conditions, and feed and product analyses are given in Table 2. As can be seen, at 9000F (4820C) and WHSV=5, near equilibrium p-xylene concentrations are achieved ( 93% of equilibrium) and xylene selectivity is very good (xylene loss is less than 1.3%). EXAMPLE 2 (Isomerization Process) A synthetic C8 aromatic feed was passed over the catalyst of Example B at temperatures between 900 and 1052 F (482 and 5670C) and WHSV between 5 and 20 and at 200 psig (1480 kPa) and H2/HC=4. The experimental conditions and feed and product analyses are summarized in Table 3. At 9000F (4820C) and WHSV=5 (Samples 1, 4 and 10), high isomerization activity is demonstrated by near equilibrium ( 92% of equilibrium) concentrations of p-xylene and the xylene selectivity is very good (xylene losses are less than 0.35%). TABLE 2 (Pressure = 200 psig [1480 kPa], H2/HC=4) Sample Feed 1 2 3 4 5 6 7 Time On Stream (hrs) 16.23 28.13 29.63 32.97 34.63 36.14 39.49 (days) 0.68 1.17 1.23 1.37 1.44 1.51 1.64 Temperature F 901 899 899 850 851 851 902 ( C) (483) (482) (482) (454) (455) (455) (483) WHSV 5 10 20 5 10 20 5 Liquid Product Analyses (Wt.%) Light Gas 1.33 0.55 0.31 0.00 0.26 0.17 0.95 Benzene 3.16 1.59 0.86 1.64 0.85 0.45 2.86 Toluene 0.10 1.00 0.43 0.25 0.48 0.28 0.19 0.80 n-C9 ethylbenzene (EB) 19.73 14.63 16.99 17.36 16.76 17.90 18.58 15.09 p-xylenea 9.46 18.26 16.80 14.28 17.93 15.64 13.36 17.99 11.8 23.2 21.1 17.6 22.33 19.49 16.63 22.71 m-xylenea 50.57 41.72 44.89 47.05 43.93 46.17 48.19 42.49 63.1 53.1 56.3 58.2 54.71 57.53 59.98 53.64 o-xylenea 20.10 18.64 18.09 19.58 18.43 18.44 18.80 18.73 25.1 23.7 22.7 24.2 22.95 22.98 23.40 23.65 <RTI ID=19.1> TABLE 2 (Continued) Sample Feed 1 2 3 4 5 6 7 Ethyl toluene (ETol) 0.26 0.11 0.04 0.03 0.03 0.03 0.10 Trimethyl benzene (TMB) 0.28 0.12 0.05 0.19 0.08 0.01 0.24 para-diethyl benzene (p-DEB) 0.40 0.25 0.14 0.37 0.20 0.10 0.40 m,o-DEB 0.03 0.01 0.01 0.02 0.01 0.00 0.03 dimethyl ethyl benzene (DMEB) 0.31 0.12 0.03 0.04 0.04 0.01 0.27 Other C9 + (total) 1.28 0.61 0.27 0.65 0.36 0.15 1.04 Total xylenes 80.13 78.62 79.78 80.90 80.29 80.25 80.35 79.21 p-xylene (% of Equilibrium) 49.2 96.8 87.7 73.5 93.0 81.20 69.3 94.6 Benzene/EB Conv. 0.83 0.77 0.48 0.74 0.62 0.52 0.82 EB/EB (%) 25.8 13.9 12.0 15.05 9.28 5.83 23.5 Xyl/Xyl (%) 1.22 0.51 0.19 0.40 0.20 0.05 0.73 Ratio 21.2 27.4 63.1 37.6 46.4 116. 32.2 a) Numbers appearing immediately below this line are percentages of the indicated xylenes in the total xylene product. TABLE 3 (Pressure = 200 psig [1480 kPa], H2/HC=4) Sample Feed 1 2 3 4 5 6 7 8 9 10 Time On Stream (hrs) 4.21 6.58 8.12 21.49 25.88 29.87 31.41 33.03 35.11 51.24 (days) 0.18 0.27 0.34 0.90 1.08 1.24 1.31 1.38 1.46 2.14 Temperature F 900 901 902 900 904 900 950 1000 1052 902 ( C) (482) (483) (483) (482) (484) (482) (510) (538) (567) (483) WHSV 5 10 20 5 7.5 20 20 20 20 Liquid Product Analyses (Wt.%) Light Gas 3.65 1.27 0.60 4.56 1.67 0.77 0.93 1.35 1.80 1.99 Benzene 4.17 2.16 1.22 5.30 2.93 1.26 2.07 3.28 4.67 4.13 Toluene 0.10 1.34 0.67 0.35 1.37 0.75 0.29 0.98 0.54 1.76 0.94 n-C9 ethylbenzene (EB) 19.73 12.50 15.93 17.28 12.51 14.86 17.42 16.42 14.66 12.53 13.69 p-xylenea 9.46 17.21 16.46 14.37 17.04 16.86 14.01 15.02 16.04 16.43 17.44 11.8 22.2 20.7 17.9 22.6 21.30 17.53 18.9 20.2 20.9 22.2 m-xylenea 50.57 43.77 42.50 48.04 42.51 45.53 47.10 46.59 45.18 44.01 44.17 63.1 56.55 56.9 59.9 56.3 57.5 58.9 58.5 57.0 56.0 56.2 o-xylenea 20.10 16.48 17.74 17.81 15.95 16.78 18.84 18.02 18.05 18.15 17.03 25.1 21.3 22.3 22.2 21.1 21.2 23.6 22.6 22.8 23.1 21.7 TABLE 3 (Continued) Sample Feed 1 2 3 4 5 6 7 8 9 10 Ethyl toluene (ETol) 0.22 0.15 0.06 0.16 0.16 0.05 0.08 0.13 0.18 0.17 Trimethyl benzene (TMB) 0.04 0.01 0.05 0.03 0.02 0.02 0.07 0.06 0.08 0.02 para-diethyl benzene (p-DEB) 0.21 0.15 0.11 0.18 0.13 0.04 0.07 0.11 0.17 0.16 m,o-DEB 0.19 0.03 0.00 0.14 0.15 0.14 0.18 0.09 0.08 0.16 dimethyl ethyl benzene (DMEB) 0.04 0.02 0.00 0.00 0.05 0.01 0.03 0.03 0.05 0.02 Other C9+ (total) 0.70 0.36 0.22 0.51 0.51 0.26 0.33 0.42 0.56 0.53 Total xylenes 77.46 79.40 80.22 75.50 79.17 79.95 79.63 79.27 78.59 78.64 p-xylene (% of Equilibrium) 92.6 86.4 74.6 94.0 88.7 73.0 78.6 84.3 87.1 92.4 Benzene/EB Conv. 0.77 0.76 0.66 0.84 0.73 0.80 0.83 0.86 0.86 0.91 EB/EB (%) 36.6 19.3 12.42 36.6 24.70 11.71 16.78 25.70 36.49 30.61 Xyl/Xyl (%) 0.30 0.17 0.14 0.20 0.22 0.09 0.22 0.25 0.34 0.20 Ratio 122.0 113.5 87.3 187.2 112.3 130.1 76.3 102.8 107.3 153.0 a) Numbers appearing immediately below this line are percentages of the indicated xylenes in the xylene product.

Claims: CLAIMS: 1. A process for isomerizing xylenes from a hydrocarbon mixture to produce a product stream comprising substantially an equilibrium mixture of para-xylene comprising contacting the hydrocarbon mixture with a catalyst comprising a ZSM-22 zeolite having a silica:alumina mole ratio of at least 20 and a Constraint Index of 2.6 at 800 F (4270C), and having the X-ray diffraction pattern of Table I. 2. A process as claimed in claim 1 wherein hydrogen is admixed with the hydrocarbon mixture such that the hydrogen to hydrocarbon mole ratio is 0.1 to 10. 3. A process--as claimed in claim 2 wherein the hydrogen to hydrocarbon mole ratio is 0.5 to 5.0. 4. A process as claimed in any preceding claim wherein the acid activity of the as-synthesized ZSM-22 zeolite has been reduced. 5. A process as claimed in claim 4 wherein the acid activity of the ZSM-22 zeolite is 5 to 50 on the Alpha scale. 6. A process as claimed in any preceding claim wherein the catalyst comprises a Group VIB or Group VIII metal. 7. A process as claimed in claim 6 wherein the metal is a noble metal of Group VIII of the Periodic Table of Elements. 8. A process as claimed in claim 7 wherein the metal is platinum or palladium. 9. A process as claimed in any one of claims 6 or 8 wherein the amount of metal in the catalyst is 0.005S by weight to 5.0% by weight, based on total catalyst weight. 10. A process as claimed in any preceding claim wherein the isomerization is conducted at the temperature of 5000F to 1100F (260 to 5930C) and at a pressure of O to 3000 psig (101 to 20785 kPa).

Inventors: CALVERT, ROBERT BRUCE, OLSON, DAVID HAROLD, VALYOCSIK, ERNEST WILLIAM
Applicants: MOBIL OIL CORPORATION
Application year: 1983
Main classification: C07C15
IPC codes: B01J29, C07B61, C07C5, C07C15, C07C67, C01B39, C07C1