Process for preparing a modified Y-zeolite

Abstract: The present invention relates to a process for preparing a modified Y-zeolite, in which an NaY-zeolite is first subjected to an ammonium exchange, the resulting ammonium exchanged zeolite is subjected to an aluminium exchange, the aluminium exchanged zeolite is subjected to a steam calcination, and a phosphorus component is incorporated into the steam calcined zeolite. The Y-zeolite obtainable by said process and an FCC catalyst comprising said Y-zeolite are also claimed. The FCC catalyst comprising the aluminium exchanged phosphorus-containing Y-zeolite according to the invention shows less coke make, and an improved selectivity to C3 olefins compared to FCC catalysts comprising zeolites which have either been aluminium exchanged or comprise phosphorus.

Description: The invention relates to a process for preparing a modified Y-zeolite, to the Y-zeolite to be obtained by said process, and to an FCC catalyst comprising said Y-zeolite. Hydrocarbon feeds can be catalytically converted to lower boiling products by being contacted with fluidised catalyst particles under appropriate conditions in a reaction zone. The catalyst used in this process is a so-called fluidised catalytic cracking (FCC) catalyst, which comprises zeolite particles in a matrix. The zeolites which have been used in the preparation of FCC catalysts include synthetic faujasites or Y-zeolites and modifications thereof, such as ultrastable Y-zeolites (USY) and calcined rare earth exchanged Y-zeolites (CREY). In the cracking process, the catalyst particles are deactivated by the precipitation of coke, which is formed as a by-product of the cracking process, on the catalyst particles. The (partially) deactivated catalyst particles are removed from the reaction zone, freed of volatile components in a stripping zone, subsequently passed to a regeneration zone, and, following their regeneration by combustion of the coke with an oxygen-containing gas, fed back to the reaction zone. In recent times, much attention has been paid to optimizing the properties of the Y-zeolites to be used in FCC catalysts, in order to obtain FCC catalysts which produce less coke and gas and are more selective to gasoline and other desirable products. One of the modifications which has been proposed is the incorporation of phosphorus into the catalyst composition. European patent application No. 0 252 761 describes a cracking catalyst comprising an ultrastable Y-zeolite which has been treated with a phosphorus-containing compound to decrease the coke and gas make of the catalyst. US patent No. 4,970,183 describes a cracking catalyst comprising a phosphorus-containing Y-zeolite which has been prepared by contacting the Y-zeolite with a phosphorus-containing compound and subsequently heating the Y-zeolite at a temperature of 400-800°C in a steam atmosphere. Again, this measure has been taken to decrease the coke and gas make of the catalyst. Another measure which has been taken to improve the properties of the catalyst is the effecting of an aluminium exchange. US patent No. 4,357,265 describes a process for modifying Y-zeolites in which an NaY-zeolite is subjected to an ammonium exchange, a calcination step, and an aluminium exchange. The FCC catalyst comprising the modified Y-zeolite produces gasoline with an improved octane number compared to a catalyst comprising a Y-zeolite which has not been subjected to an aluminium exchange. US patent No. 3,455,842 describes a cracking catalyst comprising a Y-zeolite which has been subjected to an aluminium exchange step followed by a steam calcination step. This catalyst has an improved selectivity to gasoline compared to catalysts which do not comprise aluminium exchanged Y-zeolite. US patent No. 4,224,188 describes a cracking catalyst comprising a Y-zeolite which has been prepared from an NaY-zeolite by a combination of ammonium exchange and aluminium exchange, which steps may be carried out in various orders. The activity of the FCC catalysts comprising the various zeolites is compared. However, even though the above-mentioned patents describe FCC catalysts with improved properties compared to catalysts comprising unmodified Y-zeolite, there is still need for an FCC catalyst which has an improved selectivity to gasoline and LCO, and a lower coke and gas make. An additional problem which is encountered in the use of the zeolites described in the above-mentioned references is that both the aluminium exchange step and the phosphorus treatment tend to lower the C3=/C3 ratio. Since C3 olefins are valuable products, there is need for an FCC catalyst which will show improved gasoline and LCO selectivity and decreased coke make, while the selectivity to C3 olefins is maintained or even improved. It has now been found that such an improved FCC catalyst can be obtained by incorporating therein a modified Y-zeolite prepared by a process comprising the steps of: a) exchanging an NaY zeolite with a solution of an ammonium salt in order to lower the amount of Na 2 O in the zeolite to a value below 7 wt.%; b) contacting the product obtained in step a) with an aqueous acidic aluminium-containing solution with a pH between 2 and 4, until the zeolite contains 0.5-6 wt.% of exchanged aluminium, calculated as Al 2 O 3 ; c) isolating and washing the product of step b), and calcining the resulting product in a steam atmosphere at a temperature of 450-800°C for a period of 15 minutes to 4 hours; d) treating the calcined zeolite obtained in step c) with a phosphorus-containing compound, to incorporate 0.1-4 wt.% of phosphorus, calculated as P 2 O 5 , into the zeolite. In the first step (a), a commercially available NaY-zeolite, the silica/alumina molar ratio of which preferably is between 4 and 6, is subjected to an ammonium exchange until the amount of sodium, calculated as Na 2 O, is below 7 wt.%, generally between 0.5 and 7 wt.%. Preferably, ammonium exchanging is carried out until the amount of Na 2 O is below 5 wt.%. The final amount of Na 2 O present in the zeolite should be below 1 wt.%, preferably below 0.5 wt.%. However, it is not necessary to lower the amount of Na 2 O in the zeolite to this value in this process step. Generally, it is sufficient to lower the Na 2 O content to a value between 2.5 and 5 wt.% in this process step. A further lowering of the Na 2 O content can take place after the modification of the Y-zeolite has been completed, or even after the modified Y-zeolite according to the invention has been incorporated into an FCC catalyst. The ammonium exchange can be carried out, e.g., using an ammonium sulphate solution, but other procedures known in the art may also be used. In the second step (b), the ammonium exchanged Y-zeolite obtained in step (a) is subjected to an aluminium exchange step until the zeolite contains 0.5 to 6 wt.% of exchanged aluminium, calculated as Al 2 O 3 . The percentage of exchanged aluminium present in the zeolite is defined as the difference between the percentage of aluminium, calculated as Al 2 O 3 , in the zeolite after the aluminium exchange, as determined by way of X-ray fluorescence, and the percentage of aluminium, calculated as Al 2 O 3 , in the zeolite before the aluminium exchange, also as determined by way of X-ray fluorescence. The aluminium exchange is effected by contacting the ammonium exchanged zeolite obtained in step (a) with an acidic aqueous solution containing aluminium ions. For example, a solution of a water soluble salt, such as aluminium chloride, aluminium nitrate, or aluminium sulphate may be used. The solution should have a pH value between 2 and 4. If a solution with a pH below 2 is used, the crystallinity of the zeolite will be detrimentally affected to an unacceptable extent. If a solution with a pH above 4 is used, substantial amounts of alumina will precipitate in the solution, which will affect the exchange of aluminium ions. Then, in step (c), the product of step (b) is washed in a conventional manner with water to remove excess ions. The resulting product is calcined in a steam atmosphere at a temperature of 450-700°C for a period of 15 minutes to 2 hours. It is preferred for the steam atmosphere to be saturated, but this is not necessary. Generally, the steam atmosphere will contain 10-100 wt.% of steam, preferably between 50 and 100 wt.%. It is possible to dry the washed zeolite before it is subjected to the steam calcination step, but this is not necessary. In step (d), the steam calcined zeolite obtained in step (c) is treated with phosphorus to incorporate 0.1 to 4 wt.% of phosphorus, calculated as P 2 O 5 , into the zeolite. The phosphorus treatment may be carried out, e.g., by contacting the steam calcined zeolite with an aqueous solution of a phosphorus-containing compound, such as phosphoric acid or monoammoniumdihydrogen phosphate, at a temperature between 10° and 80°C. After the treatment with phosphorus it may be advisable to carry out an extra ammonium exchange step, analogous to the one described in step (a). Whether or not such an extra step is desired will depend on the Na 2 O content of the zeolite, and on whether or not the FCC catalyst into which the modified zeolite is to be incorporated will be subjected to a washing step to remove excess ions. Although applicant does not wish to be bound by theory, it is assumed that both the aluminium exchange and the steam calcination lead to a higher amount of extra-lattice aluminium being present in the zeolite, forming condensed species. The phosphorus treatment of the zeolite results in the formation of aluminium-phosphorus compounds, which seem to confer specific catalytic properties on the zeolite. The amount of phosphorus to be incorporated into the zeolite can be related to the amount of Al° present in the zeolite. Al° is the amount of aluminium, calculated as Al 2 O 3 , determined as described by G.T. Kerr in the Journal of Physical Chemistry Vol. 71 (1967), 4155, and a measure of the amount of cationic aluminium species present in the zeolite. It is preferred that the atomic ratio between Al° and P lies in the range of 0.8 to 2.0, most preferably between 0.5 and 1.5. The invention also relates to the phosphorus-containing Y-zeolite obtainable by the process described above, which zeolite comprises 0.5-6 wt.% of exchanged aluminium, calculated as Al 2 O 3 , and 0.1-4 wt.% of phosphorus, calculated as P 2 O 5 . Preferably, said zeolite comprises 0.5 to 2.0 wt.% of exchanged aluminium, calculated as Al 2 O 3 , and 0.8 to 2 wt.% of phosphorus, calculated as P 2 O 5 . It is preferred that said zeolite has a micropore volume between 0.25 and 0.35 ml/g and a mesopore surface area between 5 and 40 m2/g, and that, after it has been deactivated for 5 hours at 788°C in a 100% steam atmosphere according to the procedure described in Example 1, the zeolite has a micropore volume between 0.1 and 0.2 ml/g, a mesopore surface area of 35-60 m2/g, and an Na content of 0.1 to 1 wt.%, calculated as Na 2 O. It is further preferred that the zeolite has a unit cell size between 2.420 and 2.430 nm, as determined according to ASTM D-3942 after deactivation at 788°C for 5 hours in a 100% steam atmosphere, according to the procedure described in Example 1. The aluminium exchanged phosphorus-containing Y-zeolite according to the invention is very suitable for use in hydrocarbon conversion catalysts, particularly FCC catalysts. The FCC catalyst will generally comprise 1-60 wt.% of the zeolite according to the invention, optionally in combination with other zeolites. The total amount of zeolite in the FCC catalyst will generally range between 10 and 60 wt.%, more in particular between 15 and 35 wt.%. The FCC catalyst comprising the modified Y-zeolite according to the invention may additionally comprise other zeolites. Examples of other zeolites which may be used in FCC catalysts in combination with the aluminium exchanged Y-zeolite according to the invention are synthetic faujasites, such as X- and Y-zeolites, as well as ZSM-5, ZSM-11, ZSM-12, ZSM-22, MCM-41, zeolite beta, hexagonal faujasites, and hydrothermally or chemically modified zeolites. If another zeolite is used in combination with the zeolite according to the invention, it is preferred to employ zeolite Y or hydrothermally or chemically modified variants thereof, such as ultrastable zeolites, which are described, int. al., in US 3 293 192, US 3 506 400, and NL 7 604 264, as well as in C.V. Mc.Daniel and P.K. Maher, Society of Chemical Engineering (London), Monograph Molecular Sieves (1968), p. 186. Preference is given to a zeolite containing a low amount of alkali metal ions, more particularly a low amount of sodium ions. The sodium ions which generally are present in freshly synthesised zeolites may be replaced through ion exchange with, say, hydrogen ions or a precursor thereof such as ammonium ions. As a rule, the ion exchange, effected on the zeolite or on the catalyst, will be performed until the zeolite, as present in the final catalyst, contains less than 4 wt.%, preferably less than 1.0 wt.%, of sodium, calculated as oxide. FCC catalysts containing the zeolite according to the invention will further contain a matrix such as silica, silica-alumina, alumina, titania, magnesia, zirconia, boria, and mixtures thereof. Preference is given to silica, silica-alumina, and alumina. It is possible to incorporate other constituents into the matrix, for instance non-ionic clays such as kaolin, bentonite clays such as described in US 3 252 757, US 3 252 889, and US 3 743 594, montmorillonite, etc. If desired it is possible to incorporate a rare earth metal component into the zeolite or the catalyst composition, using procedures which are well known in the field of preparing FCC catalysts. Optionally, the catalyst composition may contain oxidation promoters. These serve, int. al., to catalyse the reaction of CO into CO 2 during catalyst regeneration. Noble metals or compounds thereof from Group VIII of the Periodic Table, such as Pt, Pd, Ir, Rh, Os, and Ru, are especially suited, while Cr and Cu and compounds thereof are suitable also. If an oxidation promoter is employed, preference is given to 0.1-100 ppm, more particularly 0.1-50 ppm, of a noble metal from Group VIII being used. Most preferred is the use in the catalyst composition of 0.1-10 ppm of platinum or palladium. These metals may be provided on the finished FCC catalyst in a known manner, e.g., by impregnation with an appropriate salt solution, or they may be mixed with the finished catalyst composition in the form of separate particles made up, say, of platinum on alumina. If the FCC catalyst is to be used for cracking feeds which contain large amounts of metals, it may be advantageous to incorporate a metal scavenger into the FCC catalyst. This can be done by impregnating the catalyst composition with metal scavengers, e.g., alkaline earth metal components, such as salts and (hydr)oxides of barium, calcium, and magnesium. Metal passivators such as antimony compounds, tin compounds, barium titanate, and anatase can also be included in the catalyst composition in a conventional manner. The different constituents of the catalyst particles can be combined in a known manner. Suitable processes for preparing FCC catalysts are described, int. al., in US 3 609 103 and US 3 676 330. Usually, the catalyst is prepared by simply mixing all the constituents to form a slurry, followed by spray-drying. The spray-dried particles are preferably washed before use in order to remove objectionable salts. The size of the catalyst particles may be varied within wide limits. In general, FCC catalysts will have a particle size in the range of 20 to 150 µm, preferably in the range of 40 to 90 µm. Usually, the catalytic cracking of hydrocarbon feeds using an FCC catalyst is carried out at a temperature in the range of 375° to 650°C, more particularly in the range of 460° to 560°C. The pressure under which the reaction is carried out usually is in the range of atmospheric pressure to 7 atm., notably in the range of 1 to 3 atm. The oxidative regeneration of the catalyst composition with oxygen-containing gas usually is carried out at a temperature in the range of 540° to 825°C, more particularly in the range of 700° to 750°C, and in the presence of steam. The invention will be further elucidated with reference to a number of examples. First of all, various measuring techniques will be described. The surface area characteristics are obtained from the nitrogen adsorption isotherm at 78 K, which can be determined using commercially available equipment, e.g., Micromeritics A.S.A.P.-2400 or Gemini-2360. The SPESA (single point equivalent surface area) is calculated from the adsorption V a at a relative pressure P/P 0 of 0.30, according to the equation: SPESA (m 2 /g) = 4.353 (1 - P/P 0 ) V a (ml/g at standard T and P) V a is interpolated from adjacent points on the adsorption isotherm. To calculate the micro PV and the meso SA, the nitrogen adsorption isotherm in the range of P/P 0 = 0.08 to 0.80 is converted to a t-plot using the Harkins-Jura equation given by de Boer et al. ( J. Colloid Interface Sci. Vol. 21 (1966), 405), with t standing for the thickness of the adsorbed layer. t (Å) = ( 13.99 0.034 - log P/P 0 )½ Since the t-plots of zeolites are slightly curved, the part of the plot used for determining the slope and the intercept has to be specified. In the present application the range employed is from t is 0.6 nm to t is 0.9 nm. The straight line drawn through the points in this range with the aid of the least squares method has an intercept V mi and a slope ΔV a /Δt. The micro PV and the meso SA are calculated using the following formulae: micro PV (ml/g) = 0.001547 V mi meso SA (m 2 /g) = 15.47 ΔV a /Δt The chemical composition of the zeolites is determined by way of X-ray fluorescence. The sodium content is determined by atomic adsorption of the samples obtained after digestion of the zeolite with HNO 3 /HCl. The surface chemical composition was determined by way of X-ray photoelectronic spectroscopy (XPS). The crystallinity was determined by way of X-ray diffraction, with the most crystalline sample being rated at 100% crystallinity. All other crystallinity values are related to this maximum. The Si/Al atom ratio of the zeolite framework was determined from I.R. spectra. The mid-infrared region of 400-1200 cm -1 contains the fundamental vibrations of the SiO 4 and AlO 4 units in all zeolite frameworks. This area therefore contains valuable structural information on the zeolite framework. The stretching frequencies of the O-T-O bond, with T being either Si or Al, increase as the number of Al atoms in the zeolite framework decreases. Sohn et al. ( Zeolites 6 (1986), 225-227) showed that the bands in the 800 (ν 1 ) and 1050 cm -1 (ν 2 ) regions shift as the number of aluminium atoms in the unit cell varies. This variation can be used to calculate the Si/Al atom ratio of the zeolite framework from the I.R. spectrum, using the following formulae, in which ν 1 is the wavenumber (cm -1 ) of the band in the 800 cm -1 region. N Al = 0.8375 (851.60 - ν 1 ) Si/Al frame = 192 - N Al N Al The zeolite samples in the powdered form were prepared using the pellet technique by mixing and pressing under vacuum 0.7 mg of zeolite with 300 mg of potassium bromide, infrared grade, which had previously been dried at 100°C under vacuum. A Nicolet FT-IR 60 SXR spectrometer was used, and the IR signal was averaged over 32 scans for each sample, with a resolution of 4 cm -1 . Example 1 In this example an aluminium-exchanged phosphorus-containing zeolite was prepared by the process according to the invention. The starting material was an NaY-zeolite with the properties displayed in Table 1. Na 2 O (wt.%) 12.2 SPESA (m 2 /g) 720 crystallinity (%) 100 (a) 12 kg (calculated as dry weight) of said zeolite were slurried with 6.7 kg of (NH 4 ) 2 SO 4 and 6.13 kg of water. The pH of the slurry was adjusted to 4.5 by adding concentrated HCl. The acidified slurry was heated to a temperature of 80°C, and maintained at that temperature for 30 minutes with stirring, after which the zeolite was isolated from the mixture by filtration. This process was repeated twice. After the last filtration step, the filter cake was washed with water of 70°C to remove excess ammonium sulphate. (b) 3 kg (calculated as dry weight) of the ammonium exchanged zeolite prepared in step (a) were slurried in 16.3 kg water together with 195 grams of a 7.9 wt.% of Al 2 (SO 4 ) 3 solution. The pH of the resulting slurry was adjusted to a value of 3.5 using a 1 N NaOH solution. The slurry was heated to a temperature of 60°C, and maintained at that temperature for 1 hour with vigorous stirring. The aluminium exchanged zeolite was isolated by filtration, and the filter cake was washed with water of 70°C to remove excess aluminium sulphate. This resulted in an aluminium exchanged zeolite comprising 0.5% of exchanged aluminium, calculated as Al 2 O 3 . In order to prepare a zeolite comprising 1% of exchanged aluminium, 3 kg of the ammonium exchanged zeolite prepared in step (a) were slurried in an analogous manner with 390 grams of 7.9 wt.% aluminium sulphate solution. To prepare a zeolite comprising 2% of exchanged aluminium, 780 grams of 7.9 wt.% aluminium sulphate solution were used. Table 2 gives the properties of aluminium exchanged zeolites obtained in step (b) containing different amounts of aluminium. The zeolite comprising 0% of Al 2 O 3 is the zeolite obtained in step (a). In this and the following Tables, Al ex stands for the amount of aluminium, calculated as Al 2 O 3 , which has been exchanged into the zeolite. P stands for the amount of phosphorus, calculated as P 2 O 5 , incorporated into the zeolite. Si/Al frame and Si/Al surf stand for the Si/Al atom ratio in the zeolite framework and on the zeolite surface, respectively. The other abbreviations are self-explanatory. Al ex (%) PVmicro ml/g SAmeso (m 2 /g) SPESA (m 2 /g) Crystallinity (%) 0 0.35 17.0 696 100 0.5 0.35 15.0 695 94 1.0 0.33 15.0 667 91 2.0 0.33 15.0 650 86 (c) The aluminium exchanged zeolites obtained in step (b) were dried for 16 hours at 120°C. The dried samples were steam calcined at different temperatures by being contacted with steam in an open rotary oven for 1 hour. The steam calcination was carried out at 550°, 600°, and 650°C. Table 3 gives the properties of aluminium exchanged zeolites having different aluminium contents which were calcined at different temperatures. Al ex (%) Ctemp °C PVmicro ml/g SAmeso (m 2 /g) SPESA (m 2 /g) Si/Al frame Si/Al surf. Al° 0 550 0.35 27 665 4.3 1.6 0 600 0.33 39 630 5.0 1.5 0 650 0.30 47 653 5.4 1.0 2.7 0.5 550 0.30 27 614 3.8 1.4 0.5 600 0.30 41 624 4.5 2.1 2.2 0.5 650 0.26 40 555 5.0 2.5 1.0 550 0.30 32 607 3.9 2.7 1.7 1.0 600 0.29 39 607 4.5 2.0 2.2 1.0 650 0.29 41 614 5.0 1.4 2.5 2.0 550 0.28 30 584 3.9 1.9 2.0 600 0.29 35 593 4.4 1.9 2.2 2.0 650 0.27 37 570 5.0 2.7 Al° is the amount of aluminium, calculated as Al 2 O 3 , as determined by the Kerr method, which is a measure of the cationic aluminium species present in the zeolite. From a comparison between the Si/Al atom ratio in the framework and the Al° it can be concluded that: (i) steam calcination promotes the hydrolysis of framework aluminium atoms, since zeolites which have not been subjected to an aluminium exchange yet comprise cationic aluminium after steam calcination; (ii) steam calcination promotes the condensation of cationic aluminium species; as a matter of fact, zeolites calcined at even temperatures with an equal Si/Al atom ratio in the framework will have approximately the same Al° concentration after calcination, regardless of the fact that the amount of aluminium exchanged into the parent zeolites was different. This indicates that the cationic aluminium undergoes condensation upon calcination, with the condensed aluminium species not being in a form in which it will be determined by the Kerr method. It appears from Table 3 that the mesopore surface decreases as the amount of exchanged alumina present in the zeolite increases. Further, the amount of mesopore surface decreases as the amount of Al° increases. Although applicant does not wish to be bound by any theory, it seem that both these effects can be explained by the assumption that extra-framework alumina, whether derived from aluminium exchanged into the zeolite or from alumina loosened from the framework by the calcination step, will block the mesopores. (d) Phosphorus was incorporated into the steamed zeolites obtained in step (c) by way of the following procedure: 1 kilogram (based on dry weight) of each of the steam-calcined zeolites obtained in step (c) was reslurried in 3 kilograms of water at 25°C. To each slurry different amounts of a 30 wt.% aqueous solution of H 3 PO 4 were dosed. The H 3 PO 4 -treated zeolites were subsequently washed with water and dried at 120°C. The amount of phosphorus incorporated into each zeolite, calculated as P 2 O 5 , is given in Table 4. (e) The phosphorus-containing zeolites obtained in step (d) were reslurried in water, after which the slurry was ground in a colloid mill. Then, the zeolite was subjected to an ammonium exchange as described in step (a) to further reduce the amount of Na 2 O present in the zeolite. A sample of each resulting ammonium exchanged zeolite was deactivated according to the following procedure. Approximately 60 grams of zeolite sample were loaded into an 18 mm ID SANICRO 31H alloy tube. The zeolite was steamed at 788°C for 5 hours in a 100% steam atmosphere. The water flow was about 10 ml/hour. Some properties of the phosphorus-containing zeolites prepared in this step are given in Table 4. It is noted that for each of these zeolites, the steam calcination step was carried out at 600°C. Fresh zeolite Deactivated zeolite Al ex % P wt.% Na 2 O wt.% PVmicro ml/g SAmeso m 2 /g SPESA m 2 /g PVmicro ml/g SAmeso m 2 /g SPESA m 2 /g 0 0 0.49 0.31 34 641 0.19 35 400 0 1.3 0.37 0.31 13 615 0.18 41 391 0.5 0 0.45 0.30 37 632 0.17 38 377 0.5 1.2 0.38 0.30 16 598 0.17 47 382 0.5 1.4 0.41 0.32 15 631 0.17 49 383 1.0 0 0.43 0.29 35 606 0.17 36 375 1.0 1.2 0.38 0.31 16 612 0.18 51 395 1.0 1.6 0.36 0.28 12 565 0.18 53 397 2.0 0 0.56 0.28 30 577 0.16 36 337 2.0 1.4 0.44 0.27 16 541 0.17 55 376 2.0 1.9 0.40 0.26 13 520 0.15 52 344 It appears from Table 4 that the presence of phosphorus in the zeolite lowers the mesopore surface area of the fresh zeolite. However, when the zeolite is deactivated, the mesopore surface area increases with increasing phosphorus concentration. This effect becomes more pronounced as the amount of aluminium exchanged into the zeolite is increased. Without wishing to be bound by theory, applicant assumes that upon deactivation of the aluminium exchanged phosphorus-containing zeolites the extralattice alumina reacts with the phosphorus to form aluminium phosphate, which gives specific catalytic properties to the zeolite. Example 2 This example will show the improved results obtained in the catalytic cracking of hydrocarbon feeds using the aluminium exchanged phosphorus-containing zeolite according to the invention. Zeolites A to D, of which some properties are given in Table 5, were prepared by way of a process analogous to that described in Example 1, starting from the zeolite used as starting material in Example 1. More in particular, Zeolite A was prepared by carrying out steps (a), (c), and (e) of Example 1. Zeolite B was prepared by carrying out steps (a), (c), (d), and (e) of Example 1. Zeolite C was prepared by carrying out steps (a), (b), (c), and (e) of Example 1. Zeolite D was prepared by carrying out steps (a), (b), (c), (d), and (e) of Example 1. The steam calcination was carried out for a period of 1 hour at a temperature of 600°C. Al ex (%) P (wt.%) Zeolite A 0 0 Zeolite B 0 1.3 Zeolite C 2 0 Zeolite D 2 1.4 The zeolites were deactivated by being contacted with steam for 5 hours at 788°C according to the procedure described in Example 1. Catalyst discs were prepared from each of the zeolites A through D by pressing the powders in a known manner. The resulting discs were milled and sieved to select the fraction with a particle size between 0.59 and 0.84 mm. The evaluation was effected in a completely automatic MAT (microactivity test) unit. The MAT-test is described by A. Corma et al. in Applied Catalysis Vol. 66 (1990), 248. Before each run, the catalyst particles were contacted with a nitrogen flow (30 ml/min) for 20 minutes at a temperature of 482°C. A gas oil feed was fed to the upper part of the reactor with a syringe pump of continuous displacement for a contact period of 75 seconds. After each run the system was purged with nitrogen and the reaction products were collected. Between the runs, the catalyst was regenerated by being contacted with air (30 ml/min) for 3.5 hours at a temperature of 520°C. The liquid products were analysed by simulated distillation. The gaseous products were analysed by liquid chromatography. The coke formed on the catalyst was determined by measuring the amounts of carbon dioxide and water collected during the regeneration of the catalyst. The conversion was defined as the total of product gases, gasoline, LCO, and coke. The catalyst to oil ratio was varied between 0.7 and 2.0, with the amount of zeolite catalyst being maintained at 3.0 grams and the amount of gas oil feed being varied. The gas oil feed had the following distillation curve, as determined in accordance with ASTM D-1160: Percentage(wt.%) Boiling point (°C) IBP 202 5 373 10 409 20 410 30 416 40 420 50 424 60 429 70 440 80 452 90 466 FBP 479 The results of the experiments are given in Table 6. Zeolite A B C D Amount of Al ex (%) 0 0 2 2 Amount of P (wt.%) 0 1.3 0 1.4 CTO = 2 wt./wt. Conversion (wt.%) 67.5 72.7 65.9 78.5 Conv. = 65 wt.% CTO (wt./wt.) 1.8 1.3 1.9 1.1 Coke (wt.%) 5.3 3.3 4.0 2.8 C1 + C2 (wt.%) 0.8 0.8 0.8 0.8 C3 + C4 (wt.%) 6.7 6.1 7.0 6.6 Gasoline (wt.%) 37.9 39.6 38.7 39.3 LCO (wt.%) 14.3 15.2 14.6 15.5 C4=/C4 1.26 1.14 1.45 1.09 C3=/C3 4.5 4.3 4.2 4.6 isoC4 (wt.%) 0.83 0.72 0.85 0.58 From the comparison between Zeolites A and B it appears that the addition of phosphorus to the catalyst composition results in an improved conversion. Further, the sensitivity to coke formation is decreased by the addition of phosphorus, while the gasoline selectivity and the LCO selectivity are increased. From the comparison between Zeolites A and C it appears that the aluminium exchange step makes the resulting zeolite less sensitive to coke formation. From the comparison of Zeolite D, which is an aluminium exchanged phosphorus-containing zeolite according to the invention, with Zeolites B and C, which were either exchanged with aluminium or contained phosphorus, it appears that the combination of an aluminium exchange and phosphorus results in a zeolite which shows an even further improved conversion, an even more decreased coke sensitivity, and an improved C3=/C3 ratio. The last-mentioned effect is especially surprising, since both aluminium exchange and the addition of phosphorus lower the C3=/C3 ratio, as can be seen from a comparison between the results of Zeolites A and B and A and C, respectively.

Claims: A process for preparing a modified Y-zeolite which comprises: a) exchanging an NaY zeolite with a solution of an ammonium salt in order to lower the amount of Na 2 O in the zeolite to a value below 7 wt.%; b) contacting the product obtained in step a) with an aqueous acidic aluminium-containing solution with a pH between 2 and 4, until the zeolite contains 0.5-6 wt.% of exchanged aluminium, calculated as Al 2 O 3 ; c) isolating and washing the product of step b), and calcining the resulting product in a steam atmosphere at a temperature of 450-800°C for a period of 15 minutes to 4 hours; d) treating the calcined zeolite obtained in step c) with a phosphorus-containing compound, to incorporate 0.1-4 wt.% of phosphorus, calculated as P 2 O 5 , into the zeolite. A phosphorus-containing Y-zeolite obtainable by the process of claim 1, which comprises 0.5-6 wt.% of exchanged aluminium, calculated as Al 2 O 3 , and 0.1-4 wt.% of phosphorus, calculated as P 2 O 5 . A phosphorus-containing Y-zeolite according to claim 2, which comprises 0.5 to 2 wt.% of exchanged aluminium, calculated as Al 2 O 3 , and 0.8 to 2 wt.% of phosphorus, calculated as P 2 O 5 . A phosphorus-containing Y-zeolite according to claim 2 or 3, wherein the zeolite has a micropore volume between 0.25 and 0.35 ml/g and a mesopore surface area between 5 and 40 m2/g, and after it has been deactivated for 5 hours at 788°C in a 100% steam atmosphere the zeolite has a micropore volume between 0.1 and 0.2 ml/g, a mesopore surface area of 35-60 m2/g, and an Na content of 0.1 to 1 wt.%, calculated as Na 2 O. A phosphorus-containing Y-zeolite according to any one of claims 2 to 4, which has a unit cell size between 2.420 and 2.430 nm after deactivation at 788°C for 5 hours in a 100% steam atmosphere. An FCC catalyst comprising a zeolite according to any one of claims 2 to 5.

Inventors: CHAMBERLAIN OSCAR RENE, CORMA CANOS AVELINO, FALABELLA SOUZA-AGUIAR EDUARDO, CHAMBERLAIN, OSCAR RENE, CORMA CANOS, AVELINO, FALABELLA SOUZA-AGUIAR, EDUARDO, Chamberlain, Oscar René
Applicants: PETROLEO BRASILEIRO SA, PETROLEO BRASILEIRO S.A. PETROBRAS
Application year: 1995
Main classification: B01J29
IPC codes: C10G11, B01J29, C01B39