SELECTIVE ALKYLATION OF XYLENES WITH ETHYLENE

Abstract: A process for the production of 3,4-dimethyl-1-ethyl benzene by alkylation of xylene with ethylene is carried out at a temperature of 250-600°C and a pressure of 10 4/2 -10⁷N/m² in the presence of a crystalline zeolite catalyst having a silica to aluminia ratio of at least 12 and a constraint index of 2 to 12. The zeolite can be modified prior to use by steaming or coke deposition.

Description: SELECTIVE ALKYLATION OF XYLENES WITH ETHYLENE This invention is concerned with a method for the selective preparation of 3,4-dimethyl1-ethylbenzene from xylene and ethylene utilizing a shape selective zeolite catalyst. Six structural isomers of the compound dimethylethylbenzene are known to exist. The names, structures, boiling points and equilibrium distribution at 315it of these isomers are as shown below in Table I. TABLE 1 Name and Structure Boiling Equilibrium % Point, OC at 3150C 2,3-Dimethyl-l-ethylbenzene 193.9 3. 2 2,4-Dimethyl-l-ethylbenzene 188.4 16.4 2,5-Dimethyl-l-ethylbenzene 186.9 23.9 2,6-Dimethyl-l-ethylbenzene 190.0 1. 9 3,4-Dimethyl-l-ethylbenzene 189.8 20.9 3,5-Dimethyl-l-ethylbenzene 183.8 33.7 *S. Csicsery, J. of Catalysis, 19, 394 (1970) A process for the synthetic manufacture of these compounds via ethylation of xylene or of mixed xylenes in the presence of aluminium chloride is disclosed in U.S. specification 3,855,331. However, the data disclosed therein demonstrates that even at low temperatures alkylation is not selective for any particular isomer of dimethylethylbenzene. Other literature on the transalkylation of 2-ethyltoluene on H-Mordenite [S. Csicsery, Journal of Catalysis 23, 124 (1971)] indicates that the zeolite is not particularly shape selective for the production of 3,4-dimethyl-i-ethylbenzene, yielding only 30 to50% at between 200"C and 30O0C. 3,4-dimethyl-i-ethylbenzene is an intermediate useful for the production of 3,4-di- methylstyrene. A process for the selective production of 3,4-dimethyl-l-ethylbenzene would eliminate the expense and waste of presently employed processes for isolating this iosmer from equilibrium mixtures of the various dimethylethyl- benzenes. We have now discovered a process for the selective production of primarily a single desirable isomer of the six possible dimethylethylbenzene (i.e. 3,4-dimethyl-1-ethylbenzene). The process generally involves the alkylation of xylene and rearrangment of the various dimethylethyl-benzene isomers utilizing a particular type of crystalline zeolite catalyst thereby eliminating complex separation problems. Zeolite catalysts useful herein are characterized as having a silica to alumina ratio of at least about 12 and a Constraint index as hereinafter defined, of greater than 2 and up to about 12. The catalysts employed demonstrate a remarkable shape selectively to the 3,4-isomer among the various dimethylethylbenzene isomers, with the level of catalyst activity and selectivity being somewhat dependent on crystal size and steam modification. The process may be carried out by contracting the reactants with the catalyst at a temperature of about 250eC to about 600-C and a pressure of about 104 N/m2 to 107 N/M2 (0.1-100 atmospheres). The preferred temperatures and pressures will fall within the approximate range of 300 C to 450 C and 105 to 4X106 N/m , respectively. The preferred catalyst for utilization here-in comprises HZSt1-5 crystalline zeolite. The significance and manner of determination of Constraint Index are described in our British Specification 1,446,522. The class of zeolites defined herein is exemplified by ZSM-5, ZSM-11, ZSì1-23 and ZSM-35, defined respectively by the X-ray data-set forth in U.S. Specifications 3,702,886, 3,709,979, 4,076,842 and 4,016,245. The specific zeolites described, when prepared in the presence of organic cations, are substantially catalytically inactive, possible because the intra-crystalline free space is occupied by organic cations from the forming solution. They may be activated by heating in an inert atmosphere at 540cm for one hour, for example, followed by base exchange with ammonium salts followed by calcination at 540"C in air. The presence of organic cations in the forming solution may not be absolutely essential to the formation of this type zeolite; however, the presence of these cations does appear to favor the formation of this special class of zeolite. More generally, it is desirable to act-ivate this type of catalyst by base exchange with ammonium salts followed by calcination in air at about 5404C for from about 15 minutes to about 24 hours. Natural zeolites may sometimes be converted to this type zeolite catalyst by various activation procedures and other treatments such as base exchange, steaming, alumina extraction and calcination, alone or in combinations. Natural minerals which may be so treated include ferrierite, brewsterite, stilbite, dachiardite, epistilbite, heulandite, and clinoptilolite. In a preferred aspect of this invention, the zeolites hereof are selected as those having a crystal framework density, in the dry hydrogen form, of not less than about 1.6 grams per cubic centimetre. The dry density for known structures may be calculated from the number of silicon plus amonium atoms per 1000 cubic Angstroms, as given, e.g., on Page 19 of the article on Zeolite Structure by W.M. Meier, inlcuded in "Proceeings of the Conference on Molecular Sieves, London, April 1967", published by the Society of Chemical Industry, London 1968. When the crystal structure is unknown, the crystal framework density may be determined by classical pyknometer techniques. When synthesized in the alkali metal form, the zeolite is conveniently converted to the hydrogen form, generally by intermediate formation of the ammonium form as a result of ammonium ion exchange and calcination of the ammonium form to yield the hydrogen form. In addition to the hydrogen form, other forms of the zeolite wherein the original alkali metal has been reduced to less than about 1.5 percent by weight may be used. Thus, the original alkali metal of the zeolite may be replaced by ion exchange with other suitable metal cat ions of Groups I through VIII of the Periodic Table, including, by way of example, nickel, copper, zinc, palladium, calcium or rare earth metals. In practising the desired conversion process, it may be desirable to composite the above-described crystalling zeolite with another material resistant to the temperature and other conditions employed in the process. Such matrix material is useful as a binder and imparts greater resistance to the catalyst for the severe temperature, pressure and reactant feed stream velocity conditions encountered in many cracking processes. Useful matrix materials are disclosed in our European Specification 0006700. The catalysts useful herein may desirably be modified by steaming. Such treatment entails contacting the zeolite with an atmosphere containing from about 5% to about 100 steam at a temperature of from about 250"C to about 1000"C for a period of between about 0.25 and about 100 hours and under pressures ranging from subatmospheric to several hundred atmospheres. Another modifying treatment involves precoking of the catalyst to deposit a coating of between about 2 and about 75 by weight of coke thereon. Precoking can be accomplished by contacting the catalyst with a hydrocarbon charge, e.g. toluene, under high severity conditions or, alternatively, at a reduced hydrogen to hydrocarbon concentration (i.e. O to 1 mole ratio of hydrogen to hydrocarbon) for a sufficient time to deposit the desired amount of coke thereon. It has been found that the level of activity and the degree of selectivity of the preferred catalyst is dependent to some degree on the crystal size of the catalyst. Catalysts useful in the present process include a range of crystal sizes from about 0.01 to about 40 microns. The smaller crystal sizes are the most preferred in that they have been found to give the most desirable level of selectivity to the 3,4-isomer. Although crystal sizes within the entire range as set out above have been found to be useful, the most preferred catalysts will be those having a crystal size within the range of about 0.01 to 2 microns. Alkylation of xylene in the presence of the above-described catalyst is effected by contact of the xylene with ethylene at a temperature of between about 250it and about 600*C, and preferably between about 300 C and 450 C. The reaction generally takes place at atmospheric pressure, but the usable pressures may be those which fall within the approximate range of 104 N/m2 to 10 N/m2. The molar ratio of xylene to ethylene will be most preferably within the approximate range of 1:1 to 10:1. The reaction may be suitably accomplished utilizing a feed weight hourly space velocity (WHSV) of between about 0.1 and 100, preferably between about 1 and 20. The process of this invention may be conducted with the organic reactants in either the gaseous or the liquid phase, or both. It may be carried out as a batch type, semi-continuous or continuous operation utilizing a fixed, fluidized, or moving bed catalyst system. The following examples are presented by way of illustration of the process of the invention. Example 1 - Alkylation of isomeric dimethylbenzenes. A catalyst comprising of 4.0g of HZSM-5. (65 by weight) on alumina was placed in a flow reactor and heated to 3500C. A feed system consisting of mixed dimethylbenzenes (22% ortho, 55 meta, 23% para) and ethylene at a molar ratio of 3.5/1 was passed across the catalyst at a weight hourly space velocity (WHSV) of 8.6/0.65 dimethylbenzene/ethylene and atmospheric pressure. The results are shown in Table II below. TA3LE II Catalyst HZSM-5 HZSM-5 Time on Stream (hrs) 0.5 2.0 Liquid Effluent Analysis, wt%: Benzene 0.14 0.10 Toluene 1.05 0.94 Dimethylbenzenes: 1,2- 19.74 19.52 1,3 46.40 45.56 1,4- 18.90 18.38 Ethyltoluenes 1.68 1.67 l,5,5-Trimethylbenzene 0.05 0.04 l,2,4-Trimethylbenzene 0.40 0.32 Dimethylethylbenzenes: 2,3 0.19 0.21 2,4- 1.01 1.23 2,5- 0.71 0.84 3,4- 6.52 8.09 3,5- 0.51 0.51 Other 2.70 Total 100 100 Selectivity, : 3,4-DMEB/total DMEB 72.9 73.9 3,4-DMES/total Products 48.0 50.0 Example 2 (Comparison). All conditions were identical to Example 1 except the catalyst was 4.0g of an amorphous silica-alumina cracking catalyst having 90/10 SiO2/A1203. The results are shown in Table III below. TABLE III Catalyst Amorphous Silica Amorphous Silica Alumina Alumina ¯ Time on Stream (hrs) 0.5 1.0 Liquid Effluent Analysis, wt%: Benzene 0.05 Toluene 0.50 0.44 Dimethylbenzenes: 1,2- 21.53 21.62 1,3- 50.83 51.27 1,4- 20.86 20.92 Ethyltoluenes 0.18 0.10 1,3,5-Trimethylbenzene 0.19 0.17 1,2,4-Trimethylbenzene 0.52 0.40 Dimethylethylbenzenes: 2,3- 0.16 0.17 2,4- 0.95 0.90 2,5- 0.94 0.87 3,4- 1.,8 1.24 3,5- 1.42 1.25 Other 0.49 0.65 Total 100 100 Selectivity 3,4-DMEB/total DMEB 285 28.0 3,4-DMEB/total Products 21.6 21.0 As will be seen from a comparison of Examples 1 and 2, both the total yield of 3,4-DMEB and the selectivity to 3,4-DMEB relative to other isomers of DMEB have been dramatically affected by the HZSM-5 catalyst. Selectivity to the 3,4-isomer in the ZSM-5 system of Example 1 has been enhanced 260% relative to the amorphous silica-alumina system (Example 2) run under identical conditions. Example 3 (Comparison) The catalyst of Example 1 was replaced ith 4.0g of H-Mordenite (Zeolon-200H) which had been calcined at 5200C for 8 hours prior to use. The operating parameters of the reaction were otherwise identical to those of the previous examples. The results are shown in Table IV below. TABLE IV Catalyst H-Mordenite H-Mordenite Time on Stream (hrs) O. 33 1.0 Liquid Effluent Analysis, wt%: Benzene 0.09 Toluene 1.98 0.08 Dimethylbenzenes: 1,2- 19.30 23.23 1,3 46.33 54.38 1,4- 17.43 21.57 Ethyltoluenes 1.06 1,3,5-Trimethylbenzene 0.29 1,2,4-Trimethylbenzene 2.64 Dimethylethylbenzenes: 2,3- 0.18 2,4- 1.72 0.12 2,5- 1.63 0.11 3,4- 3.44 0.26 ), - 1.20 Other 2.71 0.25 Total 100 100 Selectivity, %: ,4-Diç 3/total DMEB 42.1 53.1 3,4-DMEB/total Products 22.1 45.6 As will be seen from the above results, the H-Mordenite catalyst aged quickly while on-stream and produced an isomeric mixture of dimethylethylbenzenes. Example 4 (Comparison) Rare earth-exchanged Zeolite-Y (REY) was tested under conditions identical to those of Example 1. The catalyst had been calcined for 20 hours at 5200C prior to use. The results are summarized in Table V. TABLE V Catalyst REY REY Time on Stream (hrs) 0.33 1.50 Liquid Effluent Analysis, wt%: Benzene 0.23 0.09 Toluene 7.20 3.14 Dimethylbenzenes: 1,2- 11.60 17.46 1,3 > 35.23 45.84 1,4- 13.66 17.47 Ethyltoluenes 4.56 1.28 l,3,5-Trimethylbenzene 2.79 0.84 l,2,4-Trimethylbenzene 9.80 4.13 Dimethylethylbenzenes: 2,3 0.29 0.25 2,4- 1.66 1.42 2,5- 1.57 1.28 3,4- 2.99 2.46 3,5- 3.40 .2.23 Other 5.02 2.11 Total 100 100 Selectivity, w: 3,4-DMEB/total DMEB 30.2 32.2 3,4-DMEB/total Products 7.7 12.7 Again, it will be seen that selectivity to the 3,4-DMEB is significantly less than that obtained with the HZSM-5 catalyst of Example 1. Example 5 (Comparison) Identical in all respects with Example 1 except in this instance the catalyst was 4.0g of HZSM-12 zeolite. The results are shown in Table VI below. TABLE VI Catalyst BZSM-l2 HZSM-12 Time on Stream (hrs) 0.50 1.0 Liquid Effluent Analysis, wt%: Benzene 0.13 0.08 Toluene 4.40 2.11 Dimethylbenzenes: 1,2- 18.02 20.48 1,3 42.40 48.74 1,4- 16.59 18.73 Ethyltoluenes 1.54 1.62 1,3,5-Trimethylbenzene 1.00 0.33 1,2,4-Trimethylbenzene 3.75 1.75 Dimethylethylbenzenes: : 2,3- 0.22 0.13 2,4- 1.64 1.18 2,5- 1.62 1.18 3,4- 2.97 2.10 3.5- 2.66 1.21 Other 3.06 1.21 Total 100 100 Selectivity, b 3,4-DMEB/total DMEB 32.6 35.3 3,4-DMEB/total Products 14.9 19.4 A side-by-side comparison of Table II (Example 1, HZSM-5) with Table I above (HZSM-12) reveals an unexpected clear and substantial superiority of the ZSM-5 catalyst over the ZSM-12 catalyst with respect to selectivity to 3,4-DME3 as the product of choice in the ethylation of dimethylbenzenes. ExamPles 6-12: Effect of Steaming the Catalyst. The effects of steaming the catalyst for various time periods on the conversion and selectivities for alkylation were studied and the results are summarized in Table VII below. The steamed catalysts were prepared by passing a stream of water vapor over the catalyst at 4.3cm3/hr and 600 C. The water stream was shut off after steaming for the desired time and the temperature reduced to 5500C. The catalyst was then dried in flowing air at 550"cm for 30 minutes. In each example the catalyst comprised 4.0g of HZSM-5 (65% on alumina) and the operating parameters were the same as in Example 1 - e.e. mixed dimethylbenzenes (22% ortho, 55% meta, 234 para) and ethylene at a 3.5/1 molar ratio; WHSV 8.6/0.65; reaction temperature 3500C; atmospheric pressure. TABLE VII Effect of Steaming Example Hours 5,4-DMEB 3,4-DMEB Steamed Steamed total DMEB total Products 6 None 71.5% 46.7% 7 0.50 91.5 69.7 8 1.00 91.4 75.3 9 1.25 93.0 79.5 10 1.50 92.5 80.1 11 1.75 92.5 81.1 12 2.25 92.5 81.2 Steaming the catalyst prior to use is shown to dramatically increase the selectivity to 3,4-DMEB product. A similar effect may be obtained by depositing a coating of coke on the catalyst prior to use, or by a combination of precoking and steaming the catalyst. ExamDles 1315: Alkylation of Individual Isomers of Dimethylbenzene These examples demonstrate that the selectivity to 3,4-DMEB is independent of the dimethylbenzene isomer which is used as starting material. All of the run conditions were the same as in Example 1 with the exception that the dimethylbenzene feed was substantially the isomer as indicated in Table VIII below. The catalyst was 4.0g of HZSM-5 which had been steamed for 1.75 hours at 60GeC prior to use and the DMEB/Ethylene feed WHSV was 8.6,0.65 at atmospheric pressure and 350'C. TABLE VIII Ethylation of Dimethvlbenzene Isomers Example: 13 14 15 Dimethylbenzene Isomer: 1,2- 1,3 1,4 Liauid Products: Dimethylbenzenes: 1,2- 65.46 6.00 2.79 1,3- 15.44 69.10 17.89 1,4- 4.44 7.40 65.63 3,4-DMEB 10.43 13.22 10.28 Total DMZE 10.97 14.12 10.88 Other 3.69 3.38 2.8 Se1ectivit. 96: 3,4-DMEB/total DMES 95.1 93.6 94.5 3,4-DMES/total Products 71.1 75.5 75.1 The foregoing data clearly establish that the dimethylbenzene isomers do not come to equilibrium under the conditions of the reaction. What is more, the selectivity to 3,4-DMEB products is shown to be very high regardless of the isomeric structure of the dimethylbenzene starting material. Examples 16-18: Effect of Catalyst Crystal Size The effect of crystal size on the selectivities and conversion are illustrated by the following examples, wherein samples of HZSN-5 catalyst of three different crystal sizes were studied. The runs were carried out at 350'C and atmospheric pressure, the feed stream comprising ethylene and mixed dimethylbenzenes (22% ortho, 55k meta, 23 para). The reactant feed rates and nominal crystal sizes of the zeolite catalysts are given in Table IX below, as are the test results. TABLE IX Crystal Size Effect Example: 16 17 18 Catalyst: HZSM-5 HZSM-5 HZSM-5 Nominal Crystal Size (microns): 0.02-0.05 0.2-0.5 1-2 WHSV: Dimethylbenzene 4.4 8.6 5.7 Ethylene. 0.60 0.65 0.83 Time on Stream (hrs): 6 2 1 Ethylene Conversion, mole w 46.8 39 6.9 Selectivity, : 3,4-DMES/total DMES 75.1 73.8 88.1 3,4-DMEB/total Products 76.9 50.0 26.9 The foregoing illustrates that the overall selectivity to 3,4-DMEB among all products and the rate of conversion are relatively higher for the smaller crystal size zeolites. That is to say, with respect to HZSM-5, 0.02-0.5 > 0.2-0.5 > 1-2. However, the selectivity to 3,4-DMEB relative to all DMEB isomers produced is shown to increase with increasing crystal size.

Claims: WE CLAIM: 1. A process for the selective alkylation of dimethylbenzene with ethylene to produce 3,4-dimethyl-l-ethylbenzene in excess of its normal equilibrium concentration, said process comprising ccntacting dimethylbenzene with ethylene under conditions effective for accomplishing said alkylation in the presence of a catalyst comprising a crystalline zeolite having a silica to alumina ratio of at least 12 and a constraint index of 2 to 12. 2. A process according to Claim 1 wherein said conditions comprise a temperature of 250"C to 600"C and a pressure of 104 N/m2 to 10 N/m 3. A process according to Claim 1 or Claim 2 wherein said conditions comprise a temperature between 300 C and 450"C and a pressure of 105N/m2 to 4X1o6 N/m2. 4. A process according to any preceding Claim wherein the zeolite is ZSM-5, ZSM-ll, ZSM-23 or ZSM-35. 5. A process according to any:preceding Claim wherein the zeolite is in the form of crystals less than 1 micron in size. 6. A process according to any preceding Claim wherein the zeolite is modified prior to use by steaming 7. A process according to any preceding Claim wherein the catalyst is modified prior to use by depositing between 2% and 75% by weight of coke thereon. 8. A process according to any preceding Claim wherein the zeolite constitutes 1 to 90 weight percent of a composite with a binder.

Inventors: BARILE, GEORGE CONRAD, KAEDING, WARREN WILLIAM
Applicants: MOBIL OIL CORPORATION
Application year: 1980
Main classification: C07C15
IPC codes: C07C15, B01J29, C07C1, C07C2, C07C67, C07B61