CONVERSION OF TOLUENE OVER ZEOLITE ZSM-48

Abstract: para-Disubstituted aromatics such as p-xylene, p-ethyltoluene, p-cymene are produced by alkylation or dis­ proportionation of toluene in the presence of a catalyst desig­ nated as zeolite ZSM-48.

Description: Conversion of toluene over zeolite ZSM-48 This invention relates to the use of a relatively new zeolite, ZSM-48, in catalytic hydrocarbon conversion processes, and more particularly to its use in selective production of para-dis-ubstituted aromatics. The disproportionation of aromatic hydrocarbons in the presence of zeolite catalysts has been described by Grandio et al in the Oil and Gas Journal, Vol. 69, No. 48 (1971). U.S. Patents 3,126,422; 3,413,374; 3,598,878; 3,598,879 and 3,607,961 show vapor-phase disproportionation of toluene over various catalysts. Alkylation of aromatic hydrocarbons with an oleo in in the presence of a crystalline metallic aluminosilicate having uniform pore openings of about 6 to 15 Anstrom units is described in U.S. 2,290,607. U.S. 3,251,897 describes alkylation of aromatic hydrocarbons in the presence of X- or Y-type crystalline aluminosilicate zeolites, specifically such type zeolites wherein the cation is rare earth and/or hydrogen. U.S. 3,751,504 and 3,751,506 describe vapor phase alkylation of aromatic hydrocarbons with olefins, e.g. benzene with ethylene, in the presence of a ZSM-5 type zeolite catalyst. In these prior art processes, the xylene product produced has the equilibrium composition of approximately 24 percent para, 54 percent of meta and 22 percent of ortho. The alkylation of toluene with methanol in the presence of a cation exchanged zeolite Y has been described by Yashima et al in the Journal of Catalysis 16, 273-280 (1970). These workers reported selective production of p-xylene over the approximate temperature range of 200 to 2750C. with the maximum yield of -xylene in the mixture of xylenes, i.e. about 50 percent of the xylene product mixture, being observed at 225 C. Higher temperatures were reported to result in an increase in the yield of m-xylene and a decrease in the production of para- and ortho-xylene. Transalkylation of toluene using a catalyst of faujasite- or mordenite, a Group VIII metal, such as platinum, and an additional component of arsenic, antimony, bismuth, selenium, tellurium or compounds thereof is described in U.S. 3,527,824. Of the xylene isomers, i.e. ortho, meta and para-xylene, meta-xylene is the least desired product, with ortho and para-xylene being the more desired products. p-Xylene is of particular value being useful in the manufacture of terephthalic acid which is an intermediate in the manufacture of synthetic fibers, such as "Dacron". Mixtures of xylene isomers, either alone or in further admixture with ethylbenzene, generally containing a concentration of about 24 weight percent para-xylene in the equilibrium mixture, have previously been separated by expensive superfractionation and multistage refrigeration steps. Such process, as will be realized, has involved high operation costs and has a limited yield. In accordance with the present invention, there now has been discovered that para-disubstituted aromatics such as xylene, p-ethyltoluene, and p-cymene are produced by alkylation catalyzed by a crystalline zeolite designated as ZSM-48. Zeolite ZSM-48 is described in our pending U.S. Application Serial No. 13,640, filed February 21, 1977, and in our pending European Application 80,300,463. It usually has a composition, expressed in terms of moles of anhydrous oxides per 100 moles of silica as follows: (0-15)RN : (0 1.5)M2/n0 0 : (O-2)Al203 : (l00)5i02 wherein M is at least one cation having a valence n, RN is a C1-C20 organic compound having at least one amine functional group of pKa > 7, and wherein the composition is characterized by the distinctive X-ray diffraction pattern as shown in Table l below. It is recognized that, particularly when the composition contains tetrahedral, framework aluminum, a fraction of the amine functional groups may be protonated. The doubly protonated form, in conventional notation, would be (RNH)20 and is equivalent in stoichiometry to RN + H20. The original cations can be replaced, at least in part, by calcination and/or ion exchange with another cation. Thus, the original cations are exchanged into a hydrogen or hydrogen ion precursor form or a form in which the original cation has been replaced by a- metal of Groups 2 through 8 of the Periodic Table. Thus, for example, it is contemplated to exchange the original cations with ammonium ions or with hydronium ions. Catalytically active forms of these would include, in particular, hydrogen, rare earth metals, aluminum, metals of Groups II and VIII of the Periodic Table and manganese. The X-ray diffraction pattern of ZSM-48 has the following significant lines: TABLE 1 d(A) Relative Intensity 11.9 W-S 10.2 W 7.2 W 5.9 w 4.2 VS 3.9 VS 3.6 2.85 W These values were determined by standard techniques. The radiation was the K-alpha zebu ?+ and a scintillation counter spectrometer with a strip chart pen recorder was used. The peak heights, I, and the positions as a function of 2 times theta, where theta is the Bragg angle, were read from the spectrometer chart. From these, the relative intensities, 100 I/Io, were 10 is- the intensity of the strongest line or peak, and d(obs), the interplanar spacing in A, corresponding to be- recorded lines, were calculated In Table 1 the relative intensities are given. in terms of the symbols W=weak, VS=very- strong and W-S=weak-to-strong. Ion exchange of the sodium ion with cations reveals substantially the same pattern with some minor shifts in interplanar spacing and variation in relative intensity. Other minor variations can occur depending on the- silicon to aluminum ratio of the- particular sample, as well as-if it has been subjected to thermal treatment. An overview of the typical results obtained using ZSM-48 as a catalyst for several reactions is shown below: EMI5.1 <tb> <SEP> Isomer <SEP> Dist. <tb> <SEP> WtF <SEP> In <tb> <SEP> Effluent <SEP> p <SEP> m <SEP> o <tb> 2 <SEP> 9 <SEP> cm <SEP> 5000by3 <SEP> v <SEP> < <SEP> 0.5 <SEP> 33 <SEP> 51 <SEP> 16 <tb> <SEP> (2) <SEP> (Q <SEP> w <SEP> (Equil. <SEP> 24- <SEP> 54 <SEP> 22 <tb> <SEP> I <tb> 4 <SEP> OCH=CHOH <SEP> 450 C\ <SEP> 12.6 <SEP> 50 <SEP> 30 <SEP> 20 <tb> <SEP> (1) <SEP> 3 <SEP> 3 <SEP> T <SEP> < <SEP> (equip <SEP> 24 <SEP> 54 <SEP> 22 <tb> 5.2 <SEP> &commat; <SEP> CH <SEP> CH3+CH <SEP> 2=CH2 <SEP> 3500C <SEP> > <SEP> 12.5 <SEP> 47 <SEP> 52 <SEP> 1 <tb> <SEP> (Equil. <SEP> (equi. <SEP> 32 <SEP> 50 <SEP> 18 <tb> 5.3 <SEP> QCH3+CH3CH=CH2 <SEP> 300 C; <SEP> X <SEP> 5.2 <SEP> 67 <SEP> 28 <SEP> 5 <tb> <SEP> (Equil. <SEP> 29 <SEP> 69 <SEP> 2 <tb> m <SEP> + <SEP> p <SEP> -1, <SEP> 400 C <SEP> > <SEP> Para <SEP> 85% <SEP> Conversion <tb> <SEP> Meta <SEP> 7% <SEP> Conversion <tb> As can be seen, all reactions examined exhibited significant para selectivity. Typical of the processes contemplated herein is the disproportionation of toluene to benzene- and xylenes, wherein the proportion- of para-xylene obtained is in excess- of its normal equilibrium concentration. Subs process is effectively carried out at a temperature of between about 350 and about 7500C at a pressure of between about l atmosphere and about 100 atmospheres utilizing a weight hourly space velocity of toluene of between about 0,25 and about 20. Another process- involves theimethylation of toluene by reaction of the latter with a methylating-agent, preferably methanol, at a temperature between about 250 C and about 7500C and preferably between about 3250C and about 6000C. The reaction generally takes place at atmospheric- pressure, but the pressure may be within the approximate range of 1 atmosphere to 100 atmospheres. The molar ratio of methylating agent to toluene is generally between-about 0.05 and about 5. When methanol is employed as the methylating agent a suitable molar ratio of methanol to toluene has been found to be approximately 0.1-2 moles of methanol per mole of toluene. With the use of other methylating agents, such as methylchloride, methylbromide, dimethylether, methylcarbonate, light olefins, or dimethylsulfide, the molar ratio of methylating agent to toluene may vary within the aforenoted range. Reaction is suitably accomplished utilizing a weight hourly space velocity of between about 0.1 and about 2000 and preferably between about 1 and about 100. The reaction product consisting predominantly of para-xylene or a mixture of para- and orthoxylene, together with comparatively smaller amounts of meta-xylene may be separated by any suitable means, such as by passing the same through a water condenser and subsequently passing the organic phase through a column in which chromatographic separation of the xylene isomers is accomplished. Other processes are: EMI7.1 <tb> Toluene <SEP> + <SEP> ethylene <SEP> -- > <SEP> p-ethyltoluene <SEP> <tb> Reagents and conditions are as follows Reagents: preferably ethylene; also ethanol, ethylether, ethylchloride, ethylbromide, etc. Temperature: 200-6000C; preferably 300 500 C Pressure: 0.1 atm-100 atm, preferably 1 atm - 50 atm Molar ratio of ethylating agent to toluene of about 0.05-5; preferably 0.1-2 Weight hourly space velocity of toluene of about 1-100. Toluene + propylene ) p-cymene Similarly, reagents and conditions are as follows: Reagents: preferably propylene; also isopropylalcohol, isopropylether, isopropylchloride isopropyl bromide, etc. Temperature: 150-5000C, preferably 200-4000C Pressure: 0.1 - 100 atm; preferably 1 - 50 atm Molar ratios: propylene, etc,/toluene 0.5-5; preferably 0.1-2 Weight hourly space velocity of toluene of about 1-100. A still further charge stock which can be used in the process of the present invention to obtain high yields of paraxylene includes naphthenes, such as cyclopentane, cyclohexane and alkyl cyclopentanes having at least one alkyl group of 1 to 5 carbon atoms. Typical of the naphthene reactants are methyl cyclopentane, 1,2-dimethylcyclopentane, 1,3 dimethylcyclohexane. A,nother- charge stock which can be effectively used in the present invention to selectively produce para-xylene includes paraffinic- hydrocarbons havingbetween 3 and 10 carbon atoms.- Representative of such paraffins are hutanes, pentanes, hexanes, heptanes, octanes and alkyl-substituted derivatives of these paraffins. Utilizing a paraffinic and/or naphthenic charge stock, reaction conditions include contact with the catalyst at- a temperature of between about 400 to about 7000C, a pressure between about atmospheric and about 1000 psig and a weight hourly space velocity of 0.1 to 100. The catalyst of this invention may be the product-formed by impregnation of the- zeolite powder or- pellets- with-one or more alkaline earth compounds and/or- ion exchanged with the same. Binders such as clays silica, or other inorganic oxides may be used. When such- as-used, the total catalyst composition should preferably contain at least. 50 percent by weight of crystalline aluminosilicate zeolite. When the catalyst composition has the desired physical form, it is dried and then calcined at a temperature of at least about 12000F or higher, preferably in an oxidizing atmosphere such as air. It is desirable to activate the catalyst by base exchange with ammonium salts followed by calcination in air at about 1000OF for from about 15 minutes to about 24 hours. The conversion processes described herein may be carried out as a batch type, semi-continuous or continuous operation utilizing a fixed or moving bed catalyst system. The catalyst after use may be conducted to a regeneration zone wherein coke is burned from the catalyst in an oxygen-containing atmosphere, e.g. air, at an elevated temperature, after which the regenerated catalyst is recycled to the conversion zone for further contact with the charge stock. The following examples will serve to illustrate the process of the invention without limiting the same: Examples 1 and 2 Preparation of Catalyst - A starting gel reaction mixture was prepared from sodium silicate (27.8% Si0Z·8.4% Na20, 64% H20), C7 Example 1) and Cg (Example 2) gamine compounds, sodium hydroxide and water. Crystallization was carried out in a stainless steel autoclave (1600C). After crystallization, the solids were separated from any unreacted components by filtration and then water washed followed by drying at about 1000C. Preparation of these- samples is further described in co-pending U.S. Application Serial No. 13,640, and corresponds to Examples 6 and 11 of said co-pending application. The product of Example 1 had a Si02/Al203 ratio of 1340 and a crystal size of about 1.0 micron, while for the product of Example 2, Si02/A1203 was 400 and crystal size was about 0.25 micron. As synthesized materials were worked up by calcining in helium atmosphere at 5000C for 4 hours, ammonium exchanging twice in 2N NH4NO3, and calcining in air at 5000C before use. Catalyst testing was done on 4.0 grams of catalyst at atmospheric pressure in quartz microreactors. Examples 3-8 The following reactions were conducted using the catalysts produced by the methods of Examples 1 and 2 which serve as further examples of the invention. Example 3 - Selective Toluene Disproportionation Example 4 - Alkylation of Toluene with Methanol Example 5 - Alkylation of Toluene with Ethylene Example 6 - Alkylation of Toluene with Ethylene Example 7 - Alkylation of Toluene with Propylene Example 8 - Alkylation of Toluene with Propylene Results obtained from the exercise of the foregoing examples are listed below in Tables 2 - 7, respectively. TABLE II TOLUENE DISPROPORTIONATION Catalyst: Product of Example 2 (ZSM-48) SiO2/A1203=400 Feed: Toluene Run 1 2 3 Temp. OC 400 500 550 WHSV 5.8 5.8 5.8 Product, % Lt Gas .005 .020 .029 Benzene .052 .384 1.016 Toluene 99.844 99.080 97.699 para-Xylene .035 .157 .369 meta-Xylene .026 .245 .643 ortho-Xylene .010 .081 .230 Cg+ .029 .033 .014 p/m/o XYL 49/37/14 32.5/50.7/16.8 29.7/51.8/18.5 Pressure: 1 atmosphere TABLE III ALKYLATION OF TOLUENE WITH METHANOL Catalyst: Product of Example 1 (ZSM-48) SiO2/Al203=1340 Feed: Toluene/Methanol=4 (molar ratio) Run 1 2 3 4a 5 Temp. C 350 400 450 450 400 WHSV 5.8 5.8 5.8 18.6 62 Product, % Lt Gas 0.73 0.58 0.43 0.65 0.47 Toluene 95.44 89.72 85.07 94.96 88.24 Ethylbenzene 0.03 0.03 0.03 0.03 0.03 para-Xylene 1.87 4. 38 6.33 2.20 5.20 meta-Xylene 0.93 2.44 3.71 1.09 2.81 ortho-Xylene 0.73 1.80 2.52 0.80 1.94 C9 + 0.26 1.06 1.90 0.27 1.31 Xylenes p 53.0 50.8 50.4 53.8 52.3 m 26.4 28.3 29.5 26.6 28.2 Q 20.7 20.9 20.1 19.6 19.5 a Methanol runs to 5000C + 3.5 hr calcination at 5500C prior to this run. TABLE IV ALKYLATION OF TOLUENE WITH ETHYLENE Catalyst: Product of Example 1 (ZSM-48) Si02/A1203 = 1340 Feed: Toluene/Ethylene=5.3 (molar ratio) Run 1. 2 3 Temp. C 350 450 550 Tol WHSV 6.0 6 0 6.0 Tol/Ethylene (Mole) 5.3 5.3 5.3 Product,% Lt Gas 0.32 0.29 0.27 Benzene 0.02 0.03 0.11 Toluene 98.55- 98.43 98.72 Ethylbenzene - 0.01 0.01 para-Xylene 0.05 0.03 0.06 meta-Xylene 0.02 0.02 0.05 ortho-Xylene 0.01 00.01 0.01 para-Ethyltoluene 0.70 0.80 0.38 meta-Ethyltoluene 0.16 0.37 0.38 ortho-Ethyltoluene - - 0.01 n-Pro-Tol 0.17 0.02 p/m/o - ET 81/19/0 68/32/0 50/49/1 Tol Conv., % 1.1 1.3 1.0 TABLE V ALKYLATION OF TOLUENE WITH ETHYLENE Catalyst: Product of Example 2 (ZSM-48) Si02/Al203 = 400 Feed: Toluene/Ethylene=5.2 (molar ratio) Run 1 2 3 Temp C 350 450 400 WHSV Tol 6.0 6.0 6.0 Tol/Ethylene (Mole) 5.2 5.2 5.2 Product, % Lt Gas 0.41 0.39 0.41 Benzene 0.04 0.16 0.06 Toluene 86.37 84.93 84.04 Ethylbenzene 0.08 0.10 0.06 para-Xylene 0.07 0.09 0.05 meta-Xylene 0.04 0.12 0.04 ortho-Xylene 0.02 0.04 para-Ethyltoluene 5.85 4.64 6.04 meta-Ethyltoluene 6.43 8.49 8.80 ortho-Ethyltoluene 0.19 0.94 0.43 n-Pro-Tol 0.47 0.12 0.06 p/m/o - ET 46.9/51.6/1.5 33.0/60.3/6.7 39.6/57./2.8 Tol Conv., % 13.3 14.7 15.6 TABLE VI ALKYLATION OF TOLUENE WITH PROPYLENE Catalyst: Product of Example 1 (ZSM-48) Si02/A1203=1340 Feed: Toluene/Propylene Run 1 2 3 4 Temp OC 240 300 350 345 WHSV, Tol 5.4 5.4 5.4 1.7 Tol/propylene, Mole 4.8 4.8 4.8 5 Liq. Prod., % Lt Ends 3.30 4.30 4.38 3.72 Toluene 95.78 93.90 93.53 92.81 EMI14.1 <tb> <SEP> - <SEP> 0.06 <SEP> 0.06 <SEP> 0.08 <tb> <SEP> 0.085-- <SEP> 0.046 <SEP> - <SEP> 0.074 <SEP> <tb> Cymenes <SEP> < <SEP> <SEP> m <SEP> 0.162 <SEP> 0.139 <SEP> 0.115 <SEP> 0.306 <tb> <SEP> m <SEP> 0.672 <SEP> 1.437 <SEP> 1.502 <SEP> 2.104 <tb> n-Pro-Toluene - - 0.424 0.908 p/m/o-Cymenes 73/18/9 89/9/3 93/7/- 85/12/3 Tol Conv.,% 1.0 1.9 2.2 3.6 TABLE VII ALKYLATION OF TOLUENE WITH PROPYLENE Catalyst: Product of Example 2 (ZSM-48) SiO7/A103 = 400 Feed: Toluene/Propylene 5.3 (molar ratio) Run 1 2 Temp. C 300 350 WHSV, Tol 5.9 5.9 Tol/propylene (Mole) 5.3 5.3 Product, % Lt Ends 3.46 4.18 Toluene 87.65 88.29 EB, Xyl .17 .41 EMI15.1 <tb> <SEP> o <SEP> .317 <SEP> .308 <tb> Cymenes <SEP> # <SEP> <SEP> m <SEP> 1.436 <SEP> 1.234 <tb> <SEP> Up <SEP> 3.475 <SEP> 1.401 <tb> <SEP> n-Pro--Tol, <SEP> etc. <SEP> 3.50 <SEP> 4.18 <tb> <SEP> p <SEP> 66e5 <SEP> 47*6 <SEP> <tb> Cymenes <SEP> m <SEP> <SEP> 27.5 <SEP> 41.9 <tb> <SEP> m <SEP> 6.1 <SEP> 10.5 <tb> The examples show selectivity for formation of para-isomers substantially in excess of equilibrium.

Claims: CLAIMS: 1. A process for converting toluene to products comprising a mixture of xylenes rich in p-xylene, comprising contacting toluene, optionally together with an alkylating agent, at a temperature of 150- to 7500C;, a pressure¯of '10.1325 to 10132.5kPa and a weight hourly space velocity of 0.1 to 2000 with a catalyst comprising zeolite ZSM-48. 2. A process according to claim 1 wherein toluene is disproportionated at a temperature of 350 to 7500C, a pressure of 10.325 to 10132.5kPa and a weight hourly space velocity of 0.25 to 20. 3. A process according to claim 1 wherein toluene and a methylating agent are contacted with the catalyst at. a temperature of 250 to 750 C, a pressure of 10.1325 to 10132.5kPa and a weight. hourly space velocity of 0.1 to 2000, the molar ratio of methylating agent to toluene being 0.05 to 5. 4. A process according to claim 3 wherein the methylating agent is methanol and the contacting is effected at 325 to 6000C, 1 to 100 weight hourly space velocity and a methanol/ toluene mol ratio of 0.1 to 2. 5. A process according to claim 1 wherein toluene and an ethylating agent are contacted with the catalyst at a temperature of 200 to 6000C, a pressure of 10.1325 to 10132.5kPa, a weight hourly space velocity of 1 to 100 and an ethylating agent/toluene mol ratio of 0.5 to 5. 6. A process according to claim 5 wherein the ethylating agent is ethylene and the contacting is effected at 300 to SOO0C, 10.1325 to 5066.25kPa and an ethylene/toluene mol ratio of 0.1 to 2. 7. A process according to claim 5 wherein @@@@@@@ and a propylating agent are- contacted with the catalyst at a temperature of 150 to 500 C, a pressure of 10.1325 to 1O132.5kPa, a weight hourly space velocity of 1 to 100 and a propylating agent/toluene mol ratio of 0.5 to 5. 8. A process according to claim 7 wherein the propylating agent is propylene and the contacting is effected at 200 to 4000C, 10.1325 to 5066.25kPa, and a propylene/toluene mol ratio of 0.1 to 2. 9. A process according to claim 3 wherein the methylating agent is methyl chloride or bromide, dimethyl ether, methyl carbonate, dimethylsulphide or light olefins. 10. A process according to claim 5 wherein the ethylating agent is ethanol, ethylether, or ethyl chloride or bromide. 11. A process according to claim 7 wherein the propylating agent is isopropyl alcohol, isorpropyl ether or isopropyl chloride or bromide. 12. A process according to any preceding claim wherein the zeolite ZSM-48 has a silica/alumina ratio greater than 30. 13. A process according to any preceding claim wherein the zeolite ZSM-48 has a silica/alumina ratio greater than 50. 14. A process according to any preceding claim wherein the zeolite ZSM-48 has a silica/alumina ratio greater than 400 15. A process accordinct to any proceding- claim wherein the- zeolite ZSM-48 is in the hydrogen form.

Inventors: YOUNG, LEWIS BREWSTER
Applicants: MOBIL OIL CORPORATION
Application year: 1980
Main classification: C07C6
IPC codes: C07C2, C07C6, B01J29, C07C15, C07C1, C01B39, C07B61, C07C67