HYDROCARBON CATALYTIC CRACKING CATALYST COMPOSITIONS AND METHOD THEREFOR

Abstract: A cracking catalyst for hydrocarbons with superior selec­ tivity to gasoline production and greater metals tolerance com­ prising a porous inorganic oxide matrix composited with a crystalline aluminosilicate zeolite and a phosphorus-containing alumina in the form of small lumps.

Description: Background of the Invention The present invention relates to hydrocarbon catalytic cracking catalyst compositions, in particular relates to catalyst compositions which exhibit high metals tolerance, maintain high catalytic activity and gasoline selectivity for a long period of time and can depress hydrogen and coke formation to a low level when used in catalytic cracking of heavy oil containing large amounts of heavy metals such as vanadium, nickel, iron, copper and the like and a method therefor. Catalytic cracking of hydrocarbon originally aims at the production of gasoline. Therefore, catalysts used therefor are naturally demanded to exhibit high catalytic activity and gasoline selectivity, and further metals tolerance. In recent years, it is becoming unavoidably necessary with deterioration of the oil situation to employ low grade heavy oils, typically residual oils, containing large amounts of heavy metals such as vanadium, nickel, iron, copper and the like as a feed stock for catalytic cracking. This is attaching importance to metals tolerance of catalytic cracking catalysts more and more. In catalytic cracking of heavy oils, the cracking activity and gasoline selectivity of the catalyst used therefore generally deteriorate more or less owing to deposit of metallic contaminants contained in feed oils on the catalyst. In view of this, it is customary that the usual commercially used catalytic cracking catalysts, exemplarily catalytic cracking catalysts comprising dispersing zeolite in porous inorganic oxide matrices, have such metals tolerance that can maintain a satisfactory catalytic ability even when a certain degree of metals deposit thereon. However, in catalytic cracking of the above mentioned low degree heavy oils using the catalyst of this sort, it is impossible to achieve the primary object of catalytic cracking because a large amount of metallic contaminants admixed with said oils deposit on the catalyst whereby dehydrogenation reaction is accelerated, formation of hydrogen and coke is increased, and further the crystal structure of zeolite is apt to be destroyed. Accordingly, when subjecting the low grade heavy oils containing a large amount of metallic contaminants to catalytic cracking, there have usually been employed the way of suppressing the deposit amount of metal per catalyst particle by increasing the amount of catalyst used, the way of preventing the deterioration of the catalytic activity caused by metal deposit by adding an antimony compound in the feed oil, or the like. However, these operational countermeasures can never be recommended because the running cost increases. On the other hand, as the countermeasure from the catalytic ability there has been known the one which comprises increasing the amount of zeolite to be dispersed in the catalyst than that in the normal catalytic cracking catalyst, and further U.S. Patent 4,430,199 discloses a catalytic cracking catalyst catalyst improved in metals tolerance by containing a phosphorus compound in a zeolitecontaining catalytic cracking catalyst. Still further, U.S. Patent 4,228,036 discloses a catalytic cracking catalyst prepared by dispersing zeolite in a matrix comprising alumina-aluminum phosphate-silica. In addition, U.S. Patent 3,711,422 describes that addition of an antimony compound to a catalytic cracking catalyst deactivates metallic contaminants deposited on said catalyst, and U.S. Patent 4,183,803 describes a process for passivating metallic contaminants by contacting the metallic contaminants-deposited catalyst with a compound of antimony, bismuth, phosphorus or the like. In more addition, U.S. Patent 4,222,896 proposes a catalyst comprising a MgO-Al₂O₃-AlPO₄ matrix composited with zeolite, and Japanese Laid Open Patent Application 150539/1984 proposes a catalyst comprising an alumina-magnesia matrix composited with zeolite, respectively. Of the usual catalytic cracking catalysts developed in order to improve metals tolerance thereof, the catalyst whose zeolite content has been increased can never be made a commercially attractive one. The catalyst containing a phosphorus component with or without antimony, bismuth, magnesium and the like is not necessarily satisfactory in metals tolerance. The phosphorus component and the above mentioned other metals are surely attributable to improvement in metals tolerance, but it is conjectured that the usual catalysts, wherein the phosphorus component and other metallic components are dispersed uniformly throughout the catalysts, can never obtain satisfactory results when too much metals deposit thereon because metals tolerance of the catalysts deteriorate. Our inventors have found that an alumina-containing catalytic cracking catalyst is utilized for catalytic cracking of hydrocarbon oils to deposit vanadium, and when said spent catalyst is analyzed by means of the X-ray microanalyzer the distribution of deposited vanadium well corresponds to that of alumina. This fact suggests that when alumina is allowed to be present, taking the form of small lumps, in the catalytic cracking catalyst, metallic contaminants can be deposited concentrically on its small lumps of alumina. Summary of the Invention The present invention provides a hydrocarbon catalytic cracking catalyst composition that comprises an alumina particle having a particle diameter of 10-60 µm on which a phosphorus component has previously been fixed with or without one kind or more of auxiliary components selected from the group consisting of alkali earth metals, rare earth metals, antimony, bismuth, boron, manganese and tin, a crystalline aluminosilicate zeolite and a porous inorganic oxide matrix. Further, the present invention provides a method for preparing said catalyst compositions, and said method comprises spray drying an alumina particle on which a phosphorous component has previously been fixed with or without an auxiliary component, a crystalline aluminosilicate zeolite and an aqueous slurry containing a precursor of a matrix. In the catalyst composition according to the present invention, the amount of said alumina particle on which a phosphorus component has previously been fixed with or without an auxiliary component may be controlled in the range of 5-75 wt.% of the catalytic composition, the amount of said aluminosilicate zeolite may be controlled in the range of 5-50 wt.% of the catalyst composition, and the amount of said porous inorgnic oxide matrix may be controlled in the range of 20-50 wt.% of the catalyst composition respectively. Brief Description of the Drawings Fig. 1 stands for a curve obtained by inspecting Catalyst A, prepared in Example 1 referred to afterwards and used in Example 2, by means of the X-ray microanalyzer. Fig. 2 stands for a curve obtained by inspecting Catalyst B, prepared in Comparative Example 1 and used in Example 2, by means of the X-ray microanalyzer. Description of the Preferred Embodiments The alumina particle on which, the phosphorus component is fixed with or without the auxiliary component must have a particle diameter in the range of 10-60 µm. The reason is that when using a fine alumina particle whose particle diameter is less than this range, said alumina particle disperses uniformly in the catalyst composition without existing therein in the form of small lumps of alumina, while the particle diameter more than said range is not preferable in connection with the average particle diameter of a finally obtained catalyst composition. In view of this, the alumina particle of the present invention on which the phosphorus component has been fixed is prepared by the method of contacting a previously prepared alumina or alumina hydrate having a particle diameter of 10-60 µm with a phosphoric ion (PO₄³⁻)-containing aqueous solution, drying and thereafter calcining, or by the method of contacting a coarse alumina particle or alumina hydrate with a phosphoric ion-containing aqueous solution, drying, calcining and thereafter pulverizing same into a particle diameter of 10-60 µm. When impregnating the alumina particle with the auxiliary component of the present invention together with the phosphorus component, it is possible to impregnate the above both components simultaneously using the mixed solution of a phosphoric ion-containing aqueous solution and an auxiliary component-containing aqueous solution, and it is also possible to impregnate both components separately. In the latter case, the order of impregnation does not matter, but it is preferable to dry the alumina and calcine once at the time when the first impregnation has completed. In any case, as said phosphoric ion-containing aqueous solution there can be used each aqueous solution of phosphoric acid, ammonium hydrogen phosphate, ammonium phosphate, ester phosphate or the like or their mixed solutions. As the auxiliary component-containing aqueous solution, there may be used, singly or in admixture, an aqueous solution of nitrate, carbonate, chloride or the like containing one kind or two kinds or more of alkaline earth metals, rare earth metals, antimony, bismuth, manganese and tin and an aqueous solution of boric acid. The amount of the phosphorus introduced in the alumina particle having a particle diameter of 10-60 µm is in the range of 0.6-12.2 wt.% (P/Al atomic ratio = 0.01-0.20) of alumina as elementary phosphorus, because in case said amount is less than this range there is not displayed any effect resulting from the introduction of phosphorus, while in case said amount is more than this range the pore volume of alumina decreases too much. On the other hand, when the auxiliary component of the present invention is selected from alkali earth metals and rare earth metals, the preferable amount of said auxiliary component introduced is in the range of 0.1-5 wt.% of alumina as elementary metal. In case said amount deviates from this range, expected results can never be obtained. When the auxiliary component of the present invention is selected from antimony, bismuth, boron, manganese and tin, the preferable amount of said auxiliary component introduced is in the range of 0.001-5 wt.% of alumina as elementary metal. In case said amount deviates from this range, expected results can never be obtained. The alumina particle in which the phosphorus has been introduced with or without the auxiliary component is then calcined at a temperature in the range of 250-850°C whereby the phosphorus component is fixed on the alumina particle with or without the auxiliary component. The crystalline aluminosilicate zeolite according to the present invention includes a synthetic Y-type zeolite, mordenite, a ZSM type zeolite, a natural zeolite and the like. These are used, as in the case of normal catalytic cracking catalysts, in the form ion-exchanged by the cation selected from hydrogen, ammonium and polyvalent metals. As the porous inorganic oxide, there may be used silica, silica-alumina, silica-magnesia and the like, and further there may be used also in the present invention a matrix component used usually in normal catalytic cracking catalysts. The catalyst composition of the present invention may be prepared in the same manner as the method for preparing a usual crystalline aluminosilicate zeolite catalytic cracking catalyst excepting the point of using the above mentioned specific alumina particle. That is, the catalyst composition of the present invention can be prepared by adding the above mentioned specific alumina particle having a particle diameter of 10-60 µm and the crystalline aluminosilicate zeolite to the precursor slurry of a porous inorganic oxide matrix, for instance such as silica hydrosol, silica-alumina hydrosol and the like, dispersing uniformly and spray drying the resulting mixed slurry in a usual manner. The amounts of the precursor slurry of matrix, the specific alumina particle and the crystalline aluminosilicate zeolite used are controlled so that the finally obtained catalyst composition may contain the specific alumina particle in the range of 5-75 wt.%, the crystalline aluminosilicate zeolite in the range of 5-50 wt.%, and the matrix in the range of 20-50 wt.% respectively. The spray dried particle is washed as occasion demands, and then dried again. In the catalytic cracking operation of hydrocarbon oils, metallic contaminants such as vanadium, nickel and the like admixed in the feed oil deposit on the catalyst to deteriorate the catalytic activity and gasoline selectivity of the catalyst, and further the dehydrogenating reaction caused by said deposited metals conspicuously increases the amounts of coke and hydrogen produced. In particular, vanadium moves near the crystalline aluminosilicate zeolite in the catalyst regenerating atmosphere which is normally maintained at a temperature of 630°C or more to thereby destroy its crystal structure. In the catalytic cracking catalyst compsition according to the present invention, wherein alumina particles having a particle diameter of 10-60 µm are dispersed as small lumps, metallic contaminants deposited on the catalyst are caught by said particles to aggregate thereon, and so do not disperse in the composition. Accordingly, deposited metals, in particular vanadium, are prevented from moving near the crystalline aluminosilicate zeolite even in the catalyst regenerating atmosphere maintained at 630°C or more, and consequently destruction of its crystal structure is also prevented. It is conjectured that the phosphorus fixed on alumina accelerates aggregation of metals, such as vanadium, nickel and the like, caught on alumina, and accelerates deactivation of these metals. And, when the auxiliary component selected from alkali earth metals and rare earth metals is fixed on the alumina particle, it is conjectured from the test results of the inventors of the present invention that as this auxiliary component possess very strong affinity with metal oxides such as vanadium, nickel and the like. The ability of alumina particles to catch metallic contaminants deposited on the catalyst is accelerated more and more. In case that the auxiliary component of the present invention is selected from antimony, bismuth, boron, manganese and tin, this auxiliary component readily forms a solid solution with metals such as vanadium, nickel and the like, and consequently markedly suppresses especially the dehydrating activity of nickel. Further, this auxiliary component, which is fixed on the alumina particle, has no possibility of obstructing the catalytic activity. Thus, the catalyst composition of the present invention, even when a large amount of metallic contaminants deposit thereon, can maintain high catalytic activity and high gasoline selectivity, and can suppress the production of coke and hydrogen to small amounts. Example 1 An aluminum hydroxide obtained by Bayer's process was calcined at 600°C in the air for 2 hours. Then, 500 g of this calcined alumina weighed. An aqueous phosphoric acid solution (115 ml) obtained by diluting 82 g of a 85% orthophosphoric acid with water was added to said calcined alumina and blended for 10 minutes. This phosphoric acid-added alumina particle was dried at 110°C for 17 hours, and thereafter calcined at 600°C for 1 hour, thereby preparing a phosphorus-containing alumina particle. The average particle diameter of this phosphorus-containing alumina particle was 30 µm, the phosphorus content thereof was 4.0 wt.% (0.07 in terms of P/Al atomic ratio), and the specific surface area thereof was 67 m²/g respectively. A mixed slurry was obtained by adding 500 g of said phosphorus-containing alumina particle to 4000 g of the silica hydrosol containing 5 wt.% of SiO₂ prepared by adding sulfuric acid to water glass, and further adding 300 g of a hydrogen ion-exchanged Y-type zeolite thereto. Then, this mixed slurry was spray dried, washed, and further dried to obtain a catalytic cracking catalyst composition of the present invention. This catalyst composition contained 50 wt.% of the phosphorus-containing alumina particle, 30 wt.% of the H-Y zeolite and 20 wt.% of the silica derived from the matrix, and had the average particle diameter of 68 µm. This catalyst composition is named Catalyst A. Comparative Example 1 This example relates to the usual catalyst described in U.S. Patent 4,228,036. An aluminum sulfate solution was neutralized with ammonia water, and the resulting aluminum hydroxide precipitated were washed to remove by-product salt. A 85% ortho-phosphoric acid was added, while stirring, to this alumina hydrogel slurry corresponding to the amount of 450 g as Al₂O₃ so that the phosphorus content of the alumina became 4.0%, thereby obtaining a phosphorus-containing alumina hydrogel slurry. 6250 g of said phosphorus-containing alumina hydrogel slurry was added to 4000 g of a silica hydrosol having a SiO₂ concentration of 5 wt.% prepared by adding sulfuric acid to water glass, and further 300 g of H-Y zeolite was added thereto, thereby preparing a mixed slurry. Then, this slurry was spray dried in the same manner as Example 1, washed and further dried to thereby obtain a catalytic cracking catalyst composition. This catalyst composition contained phosphorus and alumina in the total amount of 49.8 wt.%, 30.1 wt.% of H-Y zeolite and 20.1 wt.% of the silica derived from the matrix. This is named Catalyst B. Comparative Example 2 This example relates to the usual catalyst corresponding to U.S. Patent 4,430,199. A commercially available water glass No. 3 was diluted to thereby prepare a water glass solution having a SiO₂ concentration of 11.2%. A 10.5% aluminum sulfate solution was prepared separately. The water glass solution and the aluminum sulfate solution were mixed while pouring in a vessel in the ratios of 20 L/min. and 10 L/min. respectively, to thereby prepare a silica-alumina hydrogel slurry. This slurry was aged at 65°C for 3.5 hours, and then a water glass solution was added thereto for adjusting the pH to 5.8 and stabilized. Thereafter, this slurry was added with H-Y zeolite so that the zeolite content of the final catalyst composition might become 30 wt.%. The obtained mixed slurry was spray dried in the same manner as Example 1, washed and dried to obtain a phosphorus-free catalyst composition. Next, this catalyst was calcined at 600°C for 1 hour, 200 g of this calcined catalyst was impregnated with 60 g of a 22% ortho-phosphoric acid aqueous solution having the pH of 3.5 adjusted with ammonia water, and thereafter dried to thereby obtain a phosphorus-containing catalyst composition. This catalyst contained 2.0 wt.% of phosphorus, 28.6 wt.% of H-Y zeolite, and 66.8 wt.% of silica-alumina. This catalyst is named Catalyst C. Example 2 (Evaluation of catalytic performance) The above mentioned Catalysts A-C were each subjected to performance evaluation using ASTM MAT. First, for the purpose of investigating the metals tolerance of each catalyst, nickel and vanadium were deposited on each catalyst in the following manner. This is, each catalyst had previously been calcined at 600°C for 1 hour, was allowed to absorb a predetermined amount of benzene solution of nickel naphthenate and vanadium naphthenate, then dried at 110°C and thereafter calcined at 600°C for 1.5 hours. Thereafter, each catalyst steam deactivated by treating with 100% steam at 770°C for 6 hours and calcined again at 600°C for 1 hour. Each catalyst, on which nickel and vanadium had not been deposited, was treated with 100% steam at 770°C for 6 hours, and calcined at 660°C for 1 hour. The thus pretreated each catalyst was subjected to evaluation test using ASTM MAT. The obtained results are shown in Table 1. The reaction conditions used herein are as shown below. Feed oil : desulfurized vacuum gas oil Reaction temperature : 482°C Space velocity : 16 hr⁻¹ Catalyst/oil ratio : 3 (by weight) As shown in Table 1, Catalyst A corresponding to the catalyst composition of the present invention can maintain high cracking activity and high gasoline selectivity even when large amounts of metals have deposited thereon, and further can suppress the production rate of coke and hydrogen to a low level in spite of its high cracking activity. In contrast with this, Catalyst B of Comparative Example 1 and Catalyst C of Comparative Example 2 are markedly inferior in the cracking activity and gasoline selectivity because of deposition of large amounts of metals. Next, metal-deposited Catalyst A and Catalyst B were investigated about the distribution of Al, Si and V in the catalyst particle using XMA. This measurement was made according to the method described in J. Japan Petrol. Inst., vol. 26, page 344 (1983). The obtained results are shown in Fig. 1 (Catalyst A) and Fig. 2 (Catalyst B). As is evident from comparison of Fig. 1 with Fig. 2, in the case of Catalyst A, in which alumina has dispersed in the particle form, Al and V show the substantially same distribution, and this phenomenon relates that V has selectively deposited on alumina. In the case of Catalyst B, whilst, it can be seen that V has uniformly deposited in the catalyst particle. Example 3 The aluminum hydroxide (average particle diameter: 50 µm) obtained by Bayer's process was treated with phosphoric acid in the same manner as Example 1 to thereby prepare a phosphorus-containing alumina particles having the phosphorus contents of 0.008, 0.14 and 0.22 in terms of P/Al atomic ratio. These phosphorus-containing alumina particles were treated according to the same procedure as Example 1 to obtain Catalyst D, E and F containing 50 wt.% of the phosphorus-containing alumina particle, 30 wt.% of the H-Y zeolite and 20 wt. % of silica. Next, predetermined amounts of nickel and vanadium were deposited on each of these catalysts according to the same method as Example 2. The metals-tolerance of each catalyst was evaluated under the same conditions as Example 2. The results are shown in Table 2. Catalyst D and Catalyst F, in which the P/Al atomic ratio of the phosphorus-containing alumina deviates from the range of 0.01-0.20, are inferior in gasoline yield and form much coke as compared with Catalyst E. Example 4 An aqueous solution of RECl₃ corresponding to 2.1 wt.% as rare earth metal (RE) was added to the phosphorus-containing alumina particle (phosphorus content 40 wt.%, average particle diameter (30 µm) prepared in Example 1 and mixed, then dried at 110°C for 17 hours and further calcined at 600°C for 2 hours, hereby preparing an alumina particle on which RE and phosphorus had fixed. 500 g of said RE-fixed phosphorus-containing alumina particle was added to 4000 g of a 5 wt.% SiO₂-containing silica hydrosol prepared by adding phosphoric acid to a water glass, and further 300 g of hydrogen ion-exchanged Y-type zeolite was added thereto to thereby prepare a mixed slurry. Then, this mixed slurry was spray dried, washed and further dried to obtain a catalytic cracking catalyst composition according to the present invention. This catalyst composition contained 50 wt.% of the RE and phosphorus-fixed alumina particle, 30 wt.% of the H-Y zeolite, and 20 wt.% of silica derived from the matrix. This catalyst composition is named G. Example 5 A catalyst composition was prepared according to the same manner as Example 4 except that an aqueous Mg (NO₃)₂ solution was used in place of the aqueous RECl₃ solution. This catalyst composition contained 4.8 wt.% of P₂O₅, 1.2 wt.% of MgO and 44 wt.% of Al₂O₃. This catalyst is named Catalyst H. Example 6 An aluminum hydroxide (average particle diameter 50 µm) obtained by Bayer's process was treated with phosphoric acid according to the same manner as Example 1 to thereby obtain a phosphoruscontaining alumina particle, the phosphorus content of which was 8.5 wt.% (0.17 in terms of P/Al atomic ratio) of alumina. This phosphorus-containing alumina particle was added with an aqueous CaCl₂ solution correspondiong to 2.1 wt.% as Ca, and subjected to the same manner as Example 4 except that the aqueous RECl₃ solution was not employed, thereby obtaining a catalyst composition. This is named Catalyst I. Comparative Example 3 An aluminum sulfate solution was neutralized with ammonia water, and the resulting aluminum hydroxide precipitates were washed to remove by-product salt. 78 g of a 85% ortho-phosphoric acid was added, while stirring, to this alumina hydrogel slurry corresponding to the amount of 440 g as Al₂O₃, and then an aqueous magnesium nitrate solution corresponding to 12.4 g as MgO was added thereto. 4000 g of a silica hydrosol (SiO₂ concentration 5 wt.%) prepared by adding sulfuric acid to water glass was added to said slurry, and further 300 g of H-Y zeolite was added thereto to thereby prepare a mixed slurry. Then this slurry was spray dried according to the same manner as Example 1, washed and further dried to thereby obtain a catalytic cracking catalyst composition. This catalyst composition contained 4.8 wt.% of P₂O₅, 1.2 wt.% of MgO and 44 wt.% of Al₂O₃. This is named Catalyst J. Example 7 (Evaluation of catalyst performance) The above mentioned Catalysts G-J and Catalyst A obtained by Example 1 were subjected to performance evaluation using ASTM MAT in the exactly same manner as described in Example 2. The obtained results are shown in Table 3. As shown in Table 3, Catalysts G, H and I according to the present invention are high in the conversion after nickel and vanadium have deposited and the gasoline yield, and forms low coke and hydrogen as compared with the catalysts J comprising the matrix in which MgO, P₂O₅, Al₂O₃ and SiO₂ have uniformly dispersed and the zeolite. Example 8 An aqueous SbCl₃ solution corresponding to 1.2 wt.% as Sb was added to the phosphorus-containing alumina particle (phosphorus content 4.0 wt.%, average particle diameter 30 µm) prepared in Example 1 and stirred, thereafter dried at 110°C for 17 hours, and further calcined at 600°C for 2 hours, thereby preparing an alumina particle on which antimony and phosphorus had fixed. 500 g of said antimony-fixed phosphorus-containing alumina particle was added to 4000 g of a 5 wt.% SiO₂-containing silica hydrosol prepared by adding sulfuric acid to water glass, and further adding 300 g of a hydrogen ion-exchanged Y-type zeolite to prepare mixed slurry. Then, this mixed slurry was spray dried, washed and further dried to obtain a catalytic cracking catalyst composition according to the present invention. This catalyst composition contained 50 wt.% of the antimony and phosphorus-fixed alumina particle, 30 wt.% of H-Y zeolite and 20 wt.% of the silica derived from the matrix. This catalyst composition is named Catalyst K. Example 9 A catalyst composition was prepared in the same manner as Example 8 except that an aqueous Bi(NO₃)₂ solution corresponding to 1.2 wt.% as Bi was used in place of the aqueous SbCl₃ solution This catalyst composition contained 4.61 wt.% of P₂O₅, 0.67 wt.% of Bi₂O₃ and 44.7 wt.% of Al₂O₃. This catalyst composition is named Catalyst L. Comparative Example 4 An aluminum sulfate solution was neutralized with ammonia water, and the resulting aluminum hydroxide precipitates were washed to remove by-product salt. 90 g of a 85% ortho-phosphoric acid was added while stirring to this alumina hydrogel slurry corresponding to 490 g as Al₂O₃. This slurry was added with 4000 g of silica hydrosol (SiO₂ Concentration 5 wt.%) prepared by adding sulfuric acid to water glass and further added with 300 g of a H-Y zeolite to thereby prepare a mixed slurry. Then, this slurry was spray dried in the same manner as Example 1. This spray-dried one was dipped in an aqueous SbCl₃ solution (50°C) for 10 minutes, thereafter washed with water and dried to obtain a catalytic cracking catalyst composition. This catalyst composition contained 4.92 wt.% of P₂O₅, 0.72 wt.% of Sb₂O₃ and 43.5 wt.% of Al₂O₃. This catalyst composition is named Catalyst M. Example 10 (Evaluation of catalyst performance) The above mentioned Catalysts K-M and Catalyst A obtained by Example 1 were subjected to performance evaluation using ASTM MAT. First, for the purpose of investigating the metals tolerance thereof, each catalyst, nickel alone or both nickel and vanadium were deposited on each catalyst in the following manner. That is, each catalyst had previously been calcined at 600°C for 1 hour, thereafter was allowed to absorb a predetermined amount of benzene solution of nickel naphthenate or benzene solution of nickel naphthenate and vanadium naphthenate, then dried at 110°C and thereafter calcined at 600°C for 1.5 hours. Thereafter, each catalyst was steam deactivated by treating with 100% steam at 770°C for 6 hours and calcined again at 600°C for 1 hour. Each catalyst, on which nickel and vanadium had not been deposited, was treated with 100% steam at 770°C for 6 hours and then calcined at 600°C for 1 hour. The thus pretreated each catalyst was subjected to evaluation test under the same conditions described in Example 2 using ASTM MAT. The obtained results are shown in Table 4. As shown in Table 4, Catalysts K and L according to the present invention are high in the conversion and gasoline yield after nickel and vanadium have deposited, and forms low coke and hydrogen as compared with Catalyst M prepared by impregnating the antimony compound on catalyst comprising the matrix in which P₂O₅, Al₂O₃ and SiO₂ have been uniformly mixed. In addition, Catalysts K and L are high in the conversion and gasoline yield as compared with Catalyst A which contains no auxiliary component.

Claims: 1. A hydrocarbo catalytic cracking catalyst composition that comprises an alumina particle having a particle diameter of 10-60 µm on which a phosphorus component has previously been fixed, a crystalline aluminosilicate zeolite and a porous inorganic oxide matrix, wherein said phosphorus component-fixed alumina particle has a P/Al atomic ratio in the range of 0.01-0.20. 2. A catalyst composition according to claim 1, wherein said phosphorus component-fixed alumina particle contains one kind or more of auxiliary components selected from the group consisting of alkali earth metals, rare earth metals, antimony, bismuth, boron, manganese and tin. 3. A catalyst composition according to claim 2, wherein said auxiliary component is selected from alkali earth metals and rare earth metals, and the amount of the auxiliary component fixed on the alumina particle is in the range of 0.1-5 wt.% of the alumina particle. 4. A catalyst composition according to claim 2, wherein the auxiliary component is selected from antimony, bismuth, boron, manganese and tin, and the amount of the auxiliary component fixed on the alumina particle is in the range of 0.001-5 wt.% of the alumina particle. 5. A catalyst composition according to claim 1 containing the alumina particle on which the phosphorus component has previously been fixed with or without the auxiliary component in the range of 575 wt.%, the crystalline aluminosilicate zeolite in the range of 5-50 wt.% and the porous inorganic oxide matrix in the range of 20-50 wt.% respectively. 6. A method for preparing a hydrocarbon catalytic cracking catalyst composition according to any of the preceding claims comprising mixing an alumina particle having a particle diameter of 10-60 µm on which a phosphorus component has previously been fixed with or without one kind or more of auxiliary components selected from the group consisting of alkali earth metals, rare earth metals, antimony, bismuth, boron, manganese and tin and a crystalline aluminosilicate zeolite in a precursor water slurry of a porous inorganic oxide matrix; and spray drying the resulting slurry.

Inventors: IDA, TAKANORI, MASUDA, TATSUO, OGATA, MASAMITSU, SATO, GORO
Applicants: CATALYSTS & CHEMICALS INDUSTRIES CO., LTD.
Application year: 1985
Main classification: B01J29
IPC codes: B01J29, C10G11