PROCESS FOR OLIGOMERIZING LIGHT OLEFINS OR THEIR MIXTURES

Abstract: A process is disclosed for oligomerizing light olefins or their mixtures, which consists in reacting said olefins, possibly diluted with an inert gas, by means of synthetic zeolites containing oxides of silicon, titanium and aluminum, which have, in their calcined and anhydrous state, the following empirical formula: pHAlO₂ . qTiO₂ . SiO₂, wherein p has a value larger than zero and smaller than, or equal to, 0.050 and q has a value larger than zero and smaller than, or equal to, 0.025, and the H⁺ of HAlO₂ can be at least partially substitutable or substituted with cations.

Description: The present invention relates to a process for oligomerizing the light olefins by means of a particular synthetic, crystalline, porous material. Several processes for oligomerizing the olefins are known, which use synthetic zeolites as catalysts. From U.S. patents 3,756,942; 3,760,024; 3,775,501; 3,827,968; 3,960,978; 4,021,502; 4,150,062 and 4,227,992 processes are known for producing high-octane gasolines by starting from olefins by means of zeolites of "ZSM" type, i.e., zeolites constituted by silicon and aluminum oxides. The present Applicant has found that a synthetic zeolite containing oxides of silicon, titanium and aluminum is capable of oligomerizing the light olefins with a higher selectivity and a conversion than as obtained with the previously mentioned catalysts, with the temperature being the same. The object of the present invention is a process for oligomerizing light olefins, or their mixtures, which consists in reacting said olefins, possibly diluted with an inert gas, by means of synthetic zeolites containing oxides of silicon, titanium and aluminum, having in their calcined and anhydrous state, the following empirical formula: pHAlO₂ · qTiO₂ · SiO₂, wherein p has a value larger than zero or smaller than, or equal to, 0.050 and q has a value larger than zero, and smaller than, or equal to, 0.025, and the H⁺ of HAlO₂ can be at least partially substitutable, or substituted, with cations. The passage from a cationic form to another cationic form can be carried out with the usual exchange processes known from the prior art. The reaction of oligomerization is carried out at a temperature comprised within the range of from 220 to 300°C, preferably of from 230 to 270°C, under a pressure preferably comprised within the range of from 1,01 to 30,39 bars (1 to 30 abs.atm.), and at a space velocity WHSV comprised within the range of from 0.1 to 10 hours⁻¹, preferably of from 0.3 to 5 hours⁻¹. The light olefins have a number of carbon atoms comprised within the range of from 2 to 10, preferably comprised within the range of from 2 to 4. The products which are obtained by means of said process are above-all olefins and aromatic hydrocarbons containing from 5 to 20 carbon atoms. The above-defined synthetic zeolites containing oxides of silicon, titanium and aluminum result crystalline when tested by X-ray examination. Such an examination was carried out by means of a powder diffractometer equipped with an electronic pulse-counting system, using CuK α radiation. For the computation of the intensity values, the heights of the peaks were measured, and the percent value of each of them relatively to the most intense peak was computed. The main reflections for the calcined and anhydrous product are characterized by the following d values (wherein d is the interplanar distance): Said zeolites used by us show an I.R. spectrum characterized by at least the following most representative values of wn (wherein wn is the wave number): The preparation process in order to obtain said zeolites is characterized in that a derivative of silicon, a derivative of titanium, a derivative of aluminum and a nitrogenous organic base are reacted under hydrothermal conditions, with a molar ratio of SiO₂/Al₂O₃ of the reactants higher than 100, preferably comprised within the range of from 300 to 400, a molar ratio of SiO₂/TiO₂ of the reactants higher than 5, preferably comprised within the range of from 15 to 25, a molar ratio of H₂O/SiO₂ of the reactants preferably comprised within the range of from 10 to 100, more preferably comprised within the range of from 30 to 50, possibly in the presence of one or more alkali or alkali-earth salts and/or hydroxides, with a molar ratio of M/SiO₂ (wherein M is the alkali or alkali/earth cation) of the reactants lower than 0.1, preferably lower than 0.01, or zero. In the empirical formula of the material, aluminum was put in HAlO₂ form, in order to evidence that the material is in H⁺ form. When we speak in terms of the ratios of the various reactants, for aluminum the Al₂O₃ form is used, in that it is more usual. The derivative of silicon is selected from silica gel, silica sol and alkyl silicates, among which tetraethyl silicate is preferred; the derivative of titanium is selected from the salts, such as, e.g., the halides, and the organic derivatives of titanium such as, e.g., the alkyl titanates, preferably tetraethyl titanate; the derivative of aluminum is selected from the salts, such as, e.g., the halides and the hydroxides, and the organic derivatives, such as, e.g., the alkyl aluminates, preferably isopropyl aluminate. The nitrogenous organic base can be an alkylammonium hydroxide, preferably tetrapropylammonium hydroxide. In case tetrapropylammonium hydroxide is used, the TPA⁺/SiO₂ ratio (wherein TPA = tetrapropylammonium) of the reactants is comprised within the range of from 0.1 to 1, preferably of from 0.2 to 0.4. The reactants are made react by operating at a temperature comprised within the range of from 100 to 200°C, preferably of from 160 to 180°C, at a pH comprised within the range of from 9 to 14, preferably of from 10 to 12, and for a time period ranging from 1 hour to 5 days, preferably from 3 hours to 10 hours. Titanium-aluminum-silicalite is recovered by filtration or centrifugation, is washed, dried, calcined, preferably at 500-600°C for a time preferably comprised within the range of from 4 to 8 hours, and then it is exchanged into the acidic form according to the processes known from the prior art. According to another form of practical embodiment, titanium-aluminum-silicalite can be bonded with amorphous oligomeric silica, with a molar ratio of oligomeric silica/titanium-aluminum-silicalite comprised within the range of from 5: 95 to 20: 80, wherein the crystals of titanium-aluminum-silicalite are bonded in the crystal lattice by means of Si-O-Si bonds, with the mass of the crystals of titanium-aluminum-silicalite with silica being in the form of microspheres having a diamater comprised within the range of from 5 to 1000 µm. According to a further form of practical embodiment, the material obtained, as such, or in the form of microspheres, can be pelletized or extruded according to the techniques known from the art, in order to obtain pellets or extrudates having the desired size, and then calcined up to temperatures preferably contained within the range of from 500 to 600°C. Furthermore, to the titanium-aluminum-silicalite, as such, or in bonded form, a support may be added, which is selected from more or less inert materials well known in the literature, such as aluminas, kaolins, silicas, and so forth, with the amounts of said support being comprised within the range of from 10 to 40% by weight, and preferably of from 15 to 35% by weight. Finally, the blend is fabricated and calcined. The olefins used for the reaction of oligomerization, comprised within the range of from C₂ to C₁₀, can be ethylene, propylene, 1-butene, cis and trans 2-butene, isobutene, and so forth, either as individual compounds, or as mixtures. They can be furthermore used in pure form, or diluted with inert materials, such as nitrogen, methane, ethane, butane and other higher paraffins, and so forth, as well as with a portion of the reaction products. The unreacted olefins can be separated by means of any conventional methods, and recycled. The reaction of oligomerization can be carried out over a fixed bed or over a fluidized bed, at temperatures, pressures, flow rates of the reactants, which may vary within a wide range, and depend on the particular mixture fed to the reactor. In order to better illustrate the meaning of the present invention, some examples are reported, which are not to be construed as being limitative of the same invention. Example 1 This example illustrates the preparation of titanium-aluminum-silicalite. 0.2 g of aluminum isopropoxide is dissolved in 54 g of solution at 18.7% by weight of tetrapropylammonium hydroxide. Separately, 2.3 g of tetraethylorthotitanate is dissolved in 41.6 g of tetraethylsilicate, and this solution is added to the previous one with stirring. The total mass is kept heated at 50-60°C until a single-phase solution is obtained, then 100 cc of water is added. The obtained solution is charged to an autoclave, and is heated under its autogenous pressure at 170°C for 4 hours. The product is discharged and centrifuged and washed twice by re-dispersion and centrifugation, and is then dried 1 hour at 120°C, and calcined for 4 hours at 550°C in air. The composition of the reaction mixture, and the composition of the obtained products are reported in Table 1. Example 2 To a steel reactor, with an inner diameter equal to 10 mm, heated by means of an electrical oven, 1.5 cc of titanium-aluminum-silicalite prepared according to Example 1 (SiO₂/Al₂O₃ = 161; SiO₂/TiO₂ = 46), and submitted to granulation and sieving for collecting the fraction of from 20 to 40 mesh ASTM is charged. The catalyst is heated under nitrogen up to the reaction temperature, and propylene, is then fed. The reaction products are analysed by gas-chromatography, with an on-line drawing being carried out. The process conditions and the results obtained are the following: Temperature = 260°C Pressure = (1 abs.atm) 1,01 bar WHSV = 0.6 hours⁻¹ C₃H₆/N₂ ratio = 1/2 (volume/volume) C₃H₆ conversion = 98% (weight/weight) Yield of C₅ and higher olefin oligomers = 87% (weight/weight) Selectivity to % (weight/weight) C₂ = 0.2 C₃H₈ = 0.6 C₄ = 11 C₅ = 17 C₆ = 17 C₇ and higher = 54 In this, and in the following, examples, WHSV is defined as: weight of fed olefin weight of catalyst × 1 h Example 3 To the same reactor of Example 2, 1.5 cc of titanium-aluminum-silicalite prepared according to Example 1 (SiO₂/Al₂O₃ = 161; SiO₂/TiO₂ = 46), and of size of 20-40 mesh ASTM, is charged. The catalyst is heated under nitrogen up to the reaction temperature, and then propylene is fed. The reaction products are analysed on-line by gas-chromatography. The process conditions and the results obtained are the following: Temperature = 240°C Pressure = (1 abs.atm) 1,01 bar WHSV = 0.6 hours⁻¹ C₃H₆/N₂ ratio = 1/2 (volume/volume) C₃H₆ conversion = 42% (weight/weight) Yield of C₅ and higher olefin oligomers = 34% (weight/weight) Selectivity to % (weight/weight) C₂ = traces C₃H₈ = 0.3 C₄ = 18 C₅ = 22 C₆ = 32 C₇ and higher = 28 Example 4 To the same reactor of Example 2, 1.5 cc is charged of titanium-aluminum-silicalite prepared according to Example 1 (SiO₂/Al₂O₃ = 161; SiO₂/TiO₂ = 46) (granulometry of 20-40 mesh ASTM). The catalyst is heated under nitrogen up to the reaction temperature, and then 1-butene is fed. The analysis are carried out on-line by gas-chromatography. The process conditions and the results obtained are the following: Temperature = 260°C Pressure = (1 abs.atm) 1,01 bar WHSV = 0.6 hours⁻¹ 1-Butene/N₂ ratio = 1/2 (volume/volume) 1-Butene conversion = 89% (weight/weight) Yield of C₅ and higher olefin oligomers = 35% (weight/weight) Selectivity to % (weight/weight) C₂ = traces C₃ = 2 C₄ = 59 C₅ = 6 C₆ = 5 C₇ and higher = 29 (Comparative) Example 5 To the same reactor of Example 2, 1.5 cc is charged of a zeolite constituted by oxides of silicon and aluminum, with an SiO₂/Al₂O₃ ratio = 164 (granulometry of 20-40 mesh ASTM). The catalyst is heated under nitrogen up to the reaction temperature, and then propylene is fed. The analysis are carried out on-line by gas-chromatography. The process conditions and the results obtained are the following: Temperature = 260°C Pressure = (1 abs.atm) 1,01 bar WHSV = 0.6 hours⁻¹ C₃H₆/N₂ ratio = 1/2 (volume/volume) C₃H₆ conversion = 66% (weight/weight) Yield of C₅ and higher hydrocarbons = 55% (weight/weight) Selectivity to % (weight/weight) C₂ = 2 C₃H₈ = 0.9 C₄ = 14 C₅ = 13 C₆ = 16 C₇ and higher = 54 One can observe that the yield of C₅ and higher hydrocarbons is considerably lower than of Example 2. (Comparative) Example 6 To the same reactor of Example 4, 1.5 cc is charged of a ZSM-5 zeolite prepared according to Example 1 of U.S. patent 3,702,886. The catalyst is heated up to the reaction temperature, and then propylene is fed. The process conditions and the results obtained are the following: Temperature = 260°C Pressure = (1 abs.atm) 1,01 bar WHSV = 0.6 hours⁻¹ C₃H₆/N₂ ratio = 1/2 (volume/volume) C₃H₆ conversion = 63% (weight/weight) Yield of C₅ and higher olefin oligomers = 48% (weight/weight) Selectivity to % (weight/weight) C₂ = 0.2 C₃H₈ = 0.3 C₄ = 23 C₅ = 23 C₆ = 20 C₇ and higher = 33 One can observe that the yield of C₅ and higher hydrocarbons is considerably lower than of Example 2.

Claims: 1. Process for oligomerizing light olefins, or their mixtures, characterized in that said olefins having a number of carbon atoms comprised within the range of from 2 to 10, possibly diluted with an inert gas, are reacted by means of synthetic zeolites containing oxides of silicon, titanium and aluminum, having, in their calcined and anhydrous state, the following empirical formula: pHAlO₂ · qTiO₂ · SiO₂, wherein p has a value larger than zero or smaller than, or equal to, 0.050 and q has a value larger than zero, and smaller than, or equal to, 0.025, and the H⁺ of HAlO₂ can be at least partially substitutable, or substituted, with cations, with the reaction being carried out at a temperature comprised within the range of from 220 to 300°C, and at a space velocity WHSV comprised within the range of from 0.1 to 10 hours⁻¹. 2. Process according to claim 1, wherein the reaction is carried out at a temperature comprised within the range of from 230 to 270°C. 3. Process according to claim 1, wherein the reaction is carried out at a space velocity WHSV comprised within the range of from 0.3 to 5 hours⁻¹. 4. Process according to claim 1, wherein the reaction is carried out under a pressure comprised within the range of from 1,01 to 30,39 bars (1 to 30 abs.atm.). 5. Process according to claim 1, wherein the olefins have a number of carbon atoms comprised within the range of from 2 to 4. 6. Process according to claim 1, wherein the synthetic zeolites are in a form bonded with amorphous oligomeric silica, with a molar ratio of oligomeric silica/zeolites comprised within the range of from 5: 95 to 20: 80, wherein the crystals of the zeolites are mutually bonded in the crystal lattice by means of Si-O-Si bonds, with the mass of the crystals of the zeolites with silica being in the form of microspheres having a diameter comprised within the range of from 5 to 1000 µm. 7. Process according to claim 1 or 6, wherein to the synthetic zeolites a support selected from more or less inert materials is added.

Inventors: BELLUSSI, GIUSEPPE, FATTORE, VITTORIO, GIUSTI, ALDO, GUSI, STEFANO
Applicants: AGIP S.P.A., ENIRICERCHE S.P.A.
Application year: 1988
Main classification: C07C2
IPC codes: C07B61, C07C67, C07C1, C07C2, B01J29, C07C11