CN1291789C - A kind of hydrocarbon cracking catalyst containing modified faujasite - Google Patents

Abstract

A hydrocarbon cracking catalyst containing modified faujasite, wherein the modified faujasite undergoes an exchange reaction with a phosphorus compound and an ammonium compound through the faujasite, and then introduces a rare earth solution into the exchange slurry for further reaction, and is filtered , washing, and steam roasting treatment. The catalyst contains 5-45% by weight of the modified faujasite, 0-30% by weight of one or several other modified zeolites, 15-48% by weight of clay, and 15-18% by weight of clay added in addition to high temperature resistant inorganic oxides. Mix the zeolite component, clay, and the high-temperature-resistant inorganic oxide precursor added in addition to the clay evenly in a certain proportion, spray molding, and washing, and the prepared catalyst has good activity and stability, and the gasoline yield is high. Low coke yield, strong heavy oil cracking ability and heavy metal pollution resistance.

Description

A kind of hydrocarbon cracking catalyst containing modified faujasite

This application is a divisional case of a patent application with an application date of February 7, 2002, an application number of 02103910.0, and an invention title of "a modified faujasite and a hydrocarbon cracking catalyst containing the modified faujasite" Apply.

technical field

The present invention relates to a hydrocarbon cracking catalyst containing modified faujasite, more specifically, the present invention relates to a cracking catalyst containing phosphorus and rare earth elements modified zeolite, which is mainly used for the catalytic cracking reaction process of hydrocarbons .

Background technique

As the crude oil for catalytic cracking becomes heavier, it is required to improve the cracking catalyst activity and product selectivity. The activity of Y-type zeolite after rare earth exchange is greatly improved, but the selectivity of cracked products becomes worse due to the increase of hydrogen transfer activity. In order to solve the above problems, two measures have been taken. One is to reduce the rare earth content of the active components of molecular sieves, such as USP4218307 and CN87104086, and the other is to change the introduction of rare earths, such as CN86107531A, CN86107598A, and introduce them into Y-type molecular sieves in the form of precipitated rare earths. Rare earth oxides and rare earth hydroxides improve the coke selectivity and anti-heavy metal pollution performance of molecular sieve cracking catalysts to a certain extent, but the disadvantage is that the preparation process is complicated. Since the pH value of the molecular sieve exchange system is not suitable for the requirements of rare earth precipitation, the molecular sieve exchange process and the rare earth precipitation process can only be carried out step by step.

In recent years, phosphorus has been introduced into cracking catalysts to improve catalyst activity, selectivity, hydrothermal stability, anti-heavy metal pollution and anti-wear strength. These methods can be roughly divided into three categories, namely zeolite phosphorus modification, substrate phosphorus modification (see USP4584091, USP4567152, CN1070384A), catalyst post-treatment phosphorus modification (see USP4504382, CN1062157). Among them, zeolite phosphorus modification is an important development direction. At present, there are roughly three ways to modify zeolite phosphorus: exchange, impregnation and drying, and crystallization:

The methods for modifying zeolite by exchanging phosphorus include: JP62212219: NaY zeolite is exchanged with phosphorus-containing ammonium solution for many times, and roasted for many times to make P-USY zeolite with good thermal stability.

The method of modifying zeolite by impregnating phosphorus includes: EP397183, NaY zeolite is pre-exchanged with ammonium sulfate to 1-5% by weight of Na ₂ O in zeolite, and then mixed with H ₃ PO ₄ , (NH ₄ ) ₂ HPO ₄ , NH Phosphorous compounds of ₄ H ₂ PO ₄ and NaH ₂ PO ₄ are mixed and dried at pH = 4-7 and at a temperature of 20-350°C. The content of P ₂ O ₅ is 0.1-4% by weight. , 10-100% water vapor roasting to make phosphorus-containing ultra-stable Y zeolite, which improves the cracking activity of the catalyst and gasoline selectivity. Literature (J.Cat., 145, 27-36, 1994) uses H ₃ PO ₄ to impregnate USY Buddha stone, and literature (J.Cat., 132, 229-243, 1991) uses phosphorus-containing compounds to impregnate ZSM-5 zeolite , have adjusted the acidity of the zeolite molecular sieve to a certain extent, and improved the selectivity of the corresponding catalyst products.

Phosphorus modification method of zeolite through crystallization: CN1058382A introduces aluminum phosphate into the zeolite crystallization system, and directly synthesizes phosphorus-containing five-membered ring silicalite. The cracking catalyst produced has good activity stability and high gasoline octane number.

Since zeolite has its own distinctive features after phosphorus modification and rare earth modification, people have prepared zeolite molecular sieves and catalysts containing both rare earth and phosphorus. CN1147420A adopts one of REY, REHY or REX as the zeolite crystal seed, disperses the crystal seed evenly in the colloidal system composed of water glass, aluminum salt, inorganic acid and water, and synthesizes rare earth-containing zeolite with MFI structure through crystallization Molecular sieves, and then treated with phosphorus-aluminum activators at high temperatures, obtained molecular sieves containing phosphorus and rare earths, which showed excellent hydrothermal stability and good selection of low-carbon olefin products when used in high-temperature conversion reactions of hydrocarbons sex. CN1062750A treats the rare earth ultra-stable Y zeolite catalyst with an aqueous solution of a phosphorus compound, which greatly improves the cracking catalyst activity stability, cracking selectivity and anti-wear strength.

To sum up, after the cracking catalyst is modified by rare earth, phosphorus and compound modification of rare earth and phosphorus, the activity stability and cracking selectivity of the catalyst can be significantly improved. However, the shortcoming of the prior art is that the modification process is complicated. For example, the ultra-stabilization and phosphorus modification processes of zeolite are all carried out step by step, and the production cycle is long; Phosphorus modification treatment is carried out, and the utilization rate of phosphorus is low (generally lower than 60%). In order to meet the requirements of cracking catalysts for processing heavy raw oil and producing light oil products and low-carbon olefins, it is very urgent to develop new modified cracking catalysts with better performance.

Contents of the invention

The object of the present invention is to provide a hydrocarbon cracking catalyst containing rare earth and phosphorus composite modified faujasite. The modified faujasite has a simple preparation process and good activity stability; the hydrocarbon cracking catalyst containing the modified faujasite also has a relatively high gasoline yield and a low coke yield.

The present invention is achieved in the following manner:

The modified faujasite is through the exchange reaction of faujasite with phosphorus compound and ammonium compound, the weight ratio of water to zeolite is 2-25, pH=2.0-6.5, the temperature is 10-150°C, and the exchange time is 0.1-4 hours. Then introduce the rare earth solution into the exchange slurry, the reaction time is 1 to 60 minutes, filter, wash, and obtain phosphorus and rare earth modified zeolite at 250 to 800°C and 1 to 100% water vapor for 0.1 to 3.5 hours. The zeolite The unit cell constant is 2.440-2.465 nanometers, the sodium oxide is 2.0-6.5% by weight, the phosphorus is 0.01-3.0% by weight, and the rare earth oxide is 0.1-15% by weight.

The phosphorus compound of the present invention can be general orthophosphoric acid, phosphorous acid, ammonium phosphate, ammonium dihydrogen phosphate, diammonium hydrogen phosphate, aluminum phosphate, pyrophosphoric acid, can be one or more of them, the type of phosphorus compound Does not affect the implementation of the present invention; ammonium compound can be general ammonium chloride, ammonium nitrate, ammonium carbonate, ammonium bicarbonate, ammonium oxalate, ammonium sulfate, ammonium bisulfate, can be wherein one or more than one; The rare earth solution can be a mixed rare earth solution of any composition, preferably a rare earth chloride or nitrate solution.

The faujasite exchange condition of the present invention is: water and zeolite weight ratio 2～25, preferably 4～10; The weight ratio of phosphorus and zeolite in phosphorus compound is 0.001～0.10, preferably 0.002～0.06; Ammonium compound and zeolite The weight ratio is 0.05-1.0, preferably 0.1-0.8; pH=2.0-6.5, the temperature is 10-150°C, and the exchange time is 0.1-4 hours; the weight ratio of rare earth oxide and zeolite introduced in the exchange slurry is 0.001-0.2, and the reaction Filtration and washing are carried out for 1-60 minutes, and the filter cake is roasted at 250-800° C., preferably 300-700° C., under 1-100% water vapor for 0.1-3.5 hours.

Phosphorous and rare earth composite modified faujasite unit cell constant of 2.440～2.465 nanometers prepared according to the present invention, sodium oxide 2.0～6.5% by weight, phosphorus 0.01～3.0% by weight, rare earth oxide 0.1～15% by weight; wherein modified Part of the phosphorus in faujasite enters the molecular sieve through exchange, and the other part is formed by the reaction of phosphorus and rare earth to form a composite oxide that is evenly distributed on the surface of the molecular sieve. This modification has both chemical and physical effects. Structural acidity and surface properties can play a good role in modulation. In addition, the method for preparing ultra-stable modified zeolite containing phosphorus and rare earths described in the present invention also has the following characteristics:

(1) Phosphorus and rare earth elements are introduced into the zeolite molecular sieve at the same time, the process is extremely simplified, and the production cost is greatly reduced.

(2) Since phosphorus and rare earth can react stoichiometrically, the utilization rate of phosphorus and rare earth can be as high as 95%, which effectively saves raw materials.

The present invention provides a hydrocarbon cracking catalyst containing the above-mentioned modified faujasite. The catalyst consists of 5-45% by weight of modified faujasite, 0-30% by weight of one or several other modified zeolites, 15 It consists of ~48% by weight of clay and 15-18% by weight of high temperature resistant inorganic oxides added in addition to clay.

The preparation method of the catalyst can be the conventional catalyst preparation methods such as homogeneous spray molding, post-treatment, etc., by adding the above-mentioned zeolite component, clay and the precursor of the high-temperature resistant inorganic oxide in addition to the clay, so as to obtain the catalyst finished product.

The zeolite component in the catalyst composition of the present invention can be formed by using the phosphorus and rare earth modified faujasite prepared by the present invention alone, or compounded with other modified zeolites; the modified faujasite includes phosphorus and rare earth modified Y Zeolite, phosphorus and rare earth modified X zeolite; other modified zeolites are selected from one or more of X-type zeolite, Y-type zeolite, L-type zeolite, ZSM-5 zeolite, mordenite, beta zeolite, and omega zeolite. Modified zeolite obtained by physical or chemical modification, preferably modified Y-type zeolite, modified ZSM-5 zeolite; clay is kaolin, halloysite, montmorillonite, sepiolite, etc., which can be one of them or more than one. In addition to clay, the high-temperature-resistant inorganic oxides added are Al ₂ O ₃ , SiO ₂ , SiO ₂ -Al ₂ O ₃ , AlPO ₄ , MgO, which can be one or more of them; its precursors include silicon aluminum Gel, silica sol, alumina sol, silica-alumina composite sol, and pseudo-boehmite can be one or more of them.

The preparation of the catalyst can adopt conventional methods and conditions. For example, the spray drying conditions can be selected as follows: inlet temperature 300-800°C, tail gas temperature 50-350°C. The catalyst can be calcined at 200-700°C, preferably at 300-650°C, for 0.05-4 hours, preferably 0.1-3.5 hours; catalyst washing conditions can be: the weight ratio of water to catalyst is 1-35, preferably 5 ～30, washing temperature 15～100 ℃, time 0.1～2 hours, preferably 0.15～1.5 hours.

The cracking catalyst provided by the invention has the advantages of good hydrothermal stability, high reaction conversion rate and good product selectivity. At the same time, because the preparation process for preparing the modified faujasite containing rare earth and phosphorus is simple, the preparation process of the entire catalyst is greatly shortened, and the cost can be reduced by more than one-third.

Detailed ways

The following examples will further illustrate the cracking catalyst provided by the present invention and its preparation method, but these examples cannot limit the present invention.

(1) Analytical testing methods used in the present invention.

1. Unit cell constant: X-ray diffraction method.

2. Crystallinity retention rate: X-ray diffraction method.

3. Quartz content: X-ray diffraction method.

4. Kaolinite content: X-ray diffraction method.

5. Sodium oxide content: flame photometry.

6. Phosphorus content: colorimetric method

7. Rare earth oxide content: colorimetric method.

(2) raw material specification used in the embodiment of the present invention

1. Liquid ammonium phosphate 23.0 grams per liter (calculated as PO4 ^3- ); solid diammonium hydrogen phosphate; solid ammonium sulfate; solid ammonium chloride; NaY zeolite unit cell constant 2.465 nanometers, crystallinity 89% by weight: NaX zeolite unit cell Constant 2.474 nanometers, crystallinity 92% by weight; aluminum oxide 24.1% of aluminum sol, aluminum to chlorine molar ratio 1.21; silicon oxide 25.0% of silica sol; rare earth chloride solution containing rare earth oxide 200 grams per liter, rare earth nitrate containing oxide Rare earth 215 g/L, all obtained from the qualified industrial products of the Catalyst Plant of PetroChina Lanzhou Petrochemical Company.

2. ZSM-5: Ignition reduction 3.0% by weight, silicon-aluminum molar ratio 500, produced by Shanghai Fudan University; Beta zeolite: Ignition reduction 3.5% by weight, produced in Fushun, all of which are industrial qualified products.

3. Kaolin: 42.5% by weight of alumina, 3.5% by weight of quartz, 86% by weight of kaolinite; halloysite: 43.2% by weight of alumina, 2.9% by weight of quartz, and 88% by weight of kaolinite, all produced by China Kaolin Company .

4. Hydrochloric acid and sulfuric acid are analytically pure

Example 1:

Take 3 kg of NaY (dry basis), add 22.2 liters of deionized water, make a slurry, and add 1.44 kg of ammonium sulfate and 8.1 liters of ammonium phosphate. Use 3 mol/liter of hydrochloric acid to adjust the pH of the slurry to 3.8, raise the temperature, and react at 82°C for 50 minutes, then slowly add 0.90 liter of rare earth solution under stirring, continue to react for 30 minutes, filter and wash with water, and the filter cake will be cooled at 620-640°C , Calcined for 1.5 hours under the condition of 80% water vapor to obtain the modified faujasite-1 of the present invention.

With 2.50 kilograms of kaolin (dry basis), 1.74 kilograms of modified faujasite-1 and 0.20 kilograms of ZSM-5 zeolite obtained using the above-mentioned method, 3.26 kilograms of aluminum sol and 7.5 kilograms of deionized water were mixed and beaten, stirred for 1.5 hours, and passed the colloid After grinding, it is spray-dried to shape. The obtained microspheres were calcined at 400°C for 0.5 hours. Take 2 kg of calcined microspheres, add 10 kg of deionized water and 0.54 kg of ammonium sulfate, stir evenly, adjust the pH to 3.6, and wash at 60° C. for 15 minutes. After filtering, add 5 liters of ammonium phosphate and 22 kg of deionized water, stir evenly, wash at 60° C. for 15 minutes, filter and dry to obtain Phosphorous and Rare Earth Composite Modified Faujasite Cracking Catalyst-1 prepared by the present invention.

Example 2:

Take 3 kg of NaY (dry basis), add 21.0 liters of deionized water, make a slurry, and add 1.20 kg of ammonium chloride and 4.0 liters of ammonium phosphate. Use 2 mol/liter of hydrochloric acid to adjust the pH of the slurry to 3.0, raise the temperature, and react at 89°C for 30 minutes, then slowly add 0.45 liter of rare earth solution under stirring, continue to react for 30 minutes, filter and wash with water, and the filter cake will be cooled at 600-620°C , Calcined for 2.5 hours under the condition of 100% water vapor to obtain the modified faujasite-2 of the present invention.

Adopt the same condition as embodiment 1 to prepare catalyst, just change modified faujasite-1 into modified faujasite-2, add 0.20 kilograms of beta zeolite in addition, kaolin changes halloysite, add-on is constant, The phosphorus and rare earth composite modified zeolite catalyst-2 of the present invention is obtained.

Example 3:

Take 3 kilograms of NaX (dry basis), add 31.50 liters of deionized water, make a slurry, and add 1.30 kilograms of ammonium chloride and 64 grams of diammonium hydrogen phosphate. Use 2 mol/liter of hydrochloric acid to adjust the pH of the slurry to 4.0, raise the temperature, and react at 92°C for 30 minutes, then slowly add 0.31 liter of rare earth nitric acid solution under stirring, continue to react for 10 minutes, filter and wash with water, and the filter cake is at 600-620 ℃, 100% steam for 1.0 hour to obtain the modified faujasite-3 of the present invention.

With 2.45 kilograms of kaolin (dry basis), 1.5 kilograms of modified faujasite-1 and 0.40 kilograms of modified faujasite-3, 3.89 kilograms of silica sol and 7.0 kilograms of deionized water were mixed and beaten using the above method, and stirred for 1.2 hours , after passing through a colloid mill, it is spray-dried and shaped. The resulting microspheres were calcined at 410°C for 0.6 hours. Take 2 kg of calcined microspheres, add 10 kg of deionized water and 0.54 kg of ammonium sulfate, stir evenly, adjust the pH to 3.6, and wash at 60° C. for 15 minutes. After filtering, add 4.5 liters of ammonium phosphate and 21 kg of deionized water, stir evenly, wash at 60° C. for 15 minutes, filter and dry to obtain the modified faujasite cracking catalyst-3 prepared by the present invention.

Comparative example 1:

Take 3 kg of NaY (dry basis), add 21.0 liters of deionized water, beat, add 1.20 kg of ammonium chloride, 4.0 liters of ammonium phosphate and 0.45 liters of rare earth solution, mix well, adjust the pH of the slurry with 2 mol/liter of hydrochloric acid 3.5, heat up, react at 89°C for 40 minutes, filter, wash with water, roast the filter cake at 600-620°C, 100% steam for 2.5 hours; add 15 liters of deionized water and 4.0 liters of ammonium phosphate to the molecular sieve after roasting , mix evenly, use 2 mol/liter of hydrochloric acid to adjust the pH of the slurry to 3.5, raise the temperature, react at 89° C. for 40 minutes, filter, wash with water, and dry to obtain comparatively modified faujasite-a.

The catalyst was prepared under the same conditions as in Example 1, except that the modified faujasite-1 was changed to the above-mentioned modified faujasite a, and the addition amount was unchanged, so that comparative catalyst-A was prepared.

The modified faujasite and catalyst obtained in Examples 1-3 and Comparative Example 1 were evaluated and compared as follows.

1. Comparison of physical and chemical properties of modified faujasite.

Table 1 is a comparison of the physical and chemical properties of modified zeolites,

Table 1 Comparison of physical and chemical properties of modified zeolites project Example comparative example Modified Faujasite-1 Modified Faujasite-2 Modified Faujasite-3 Modified faujasite-a Sodium oxide, wt% 4.60 4.10 4.85 4.50 Rare earth oxides, % by weight 5.70 2.95 2.02 2.25 Phosphorus, % by weight 1.90 0.93 0.48 0.50 Unit cell constant, nm 2.460 2.459 2.466 2.462 Phosphorus utilization rate, %① 95 93 96 50 Rare earth utilization rate, %② 95 98 98 75 Zeolite stability, %③ 45 46 43 44

① Refers to the phosphorus content in the molecular sieve ÷ the theoretical dosage of phosphorus.

② Refers to the rare earth content in the molecular sieve ÷ the theoretical dosage of rare earth.

③ Refers to the crystallinity of aged molecular sieve (800°C*4 hours, 100% water vapor) ÷ the crystallinity of fresh molecular sieve × 100%.

As can be seen from Table 1, in the modified faujasite 1-3 that embodiment 1-3 applies the preparation technology of the present invention to obtain, phosphorus and rare earth can produce precipitation reaction stoichiometrically, and the utilization rate of phosphorus and rare earth can reach 90% % or more, while the rare earth utilization rate of the modified faujasite a obtained by the process of the comparative example is 75%, and the phosphorus utilization rate is only about 50%, and its preparation process is complicated in the comparative example. Therefore, the phosphorus and rare earth compound modified faujasite provided by the invention has good stability, simple preparation process and high utilization rate of phosphorus and rare earth.

2. Measure the anti-vanadium reactivity of the cracking catalysts 1-3 of the present invention and comparative catalyst A by micro-inversion experiments.

Experimental conditions: 800°C, 100% steam for 4 hours, then react at 460°C for 70 seconds. The catalyst loading is 5.0g, the catalyst-to-oil ratio is 3.2, the raw material oil is straight-run light diesel oil, and the oil intake is 1.56g.

Get 5.74 grams of ammonium metavanadate and dissolve in 3% aqueous hydrogen peroxide solution to prepare 500 milliliters of vanadium-containing 0.5% solution. The catalyst was contaminated with vanadium according to Mitchell's method (Ind. Eng. Chem. Prod. Dev. 19, 209, 1980). The catalyst was first calcined at 540°C for 1.5 hours, soaked in the above-mentioned vanadium solution at room temperature for 16 hours, dried at 120°C for 24 hours, then calcined at 540°C for 4 hours, and then the microreaction activity of the contaminated catalyst was measured.

Catalysts 1 to 3 and catalyst A obtained in Examples 1 to 3 and Comparative Examples were subjected to micro-inversion experiments, and the results are shown in Table 2.

Table 2 Micro-reactor experiment and pollution data of the catalyst ^* project Example comparative example Catalyst-1 Catalyst-2 Catalyst-3 Catalyst-A Microreactivity, % Before pollution 74 75 73 71 After pollution 55 56 53 50 Activity retention rate, % 74 75 73 70

^* Pollution level: Vanadium = 5000ppm

It can be seen from Table 2 that compared with the contrast agent, the cracking catalysts 1-3 prepared by the present invention have higher micro-reaction activity, and under the condition of 5000ppm vanadium pollution, the activity retention rate is higher by 4-5 units.

3. Measure the cracking reaction selectivity of cracking catalyst 1～3 of the present invention and comparative catalyst-A by fixed fluidized bed experiment

Experimental conditions: aging at 800°C and 100% water vapor for 10 hours, reaction temperature 500°C, regeneration temperature 650°C, weight space velocity 16h ^-1 , catalyst loading 150g, agent-oil ratio 3.75, raw oil 70 % wide distillate + 30% Xinjiang vacuum residue. The fixed bed evaluation results are shown in Table 3.

It can be seen from Table 3 that compared with comparative catalyst-A, catalysts 1-3 prepared by the present invention have high gasoline yield and low heavy oil yield, and simultaneously have good coke selectivity.

Table 3 Evaluation data of fixed fluidized bed project Example comparative example Catalyst-1 Catalyst-2 Catalyst-3 Catalyst-A Dry gas, wt% 1.5 1.5 1.4 1.6 Liquefied gas, wt% 23.6 22.0 22.5 22.7 Gasoline, % by weight 47.0 48.5 47.6 45.9 Diesel, wt% 15.2 15.2 15.0 15.6 Heavy oil, wt% 7.1 8.0 7.5 8.6 Coke, wt% 3.8 3.2 3.6 3.9 Conversion, % by weight 75.9 75.2 75.1 74.1 coke/conversion 0.050 0.043 0.048 0.053

Claims (7)

1. hydrocarbon cracking catalyzer that contains modcfied faujasite is characterized in that: catalyst is made up of the modcfied faujasite of 5～45 weight %, one or more other modified zeolites of 0～30 weight %, the clay of 15～48 weight % and the high-temperature inorganic oxide that 15～18 weight % add except that clay in addition; Wherein modcfied faujasite is meant by faujasite and phosphorus compound and ammonium compounds and carries out exchange reaction, water and zeolite weight ratio 2～25, pH=2.0～6.5, temperature is 10～150 ℃, be 0.1～4 hour swap time, in the exchange slurries, introduce earth solution then, 1～60 minute reaction time, after filtration, washing, through phosphorus and rare earth modified zeolite at 250～800 ℃, roasting 0.1～3.5 hour under 1～100% steam and obtaining, these zeolite lattice constant 2.440～2.465 nanometers, sodium oxide molybdena 2.0～6.5 weight %, phosphorus 0.01～3.0 weight %, rare earth oxide 0.1～15 weight %.

2. hydrocarbon cracking catalyzer according to claim 1 is characterized in that described phosphorus compound is selected from one or more in orthophosphoric acid, phosphorous acid, ammonium phosphate, ammonium dihydrogen phosphate (ADP), diammonium hydrogen phosphate, aluminum phosphate, the pyrophosphoric acid.

3. hydrocarbon cracking catalyzer according to claim 1 is characterized in that described ammonium compounds is selected from one or more in ammonium chloride, ammonium nitrate, ammonium carbonate, carbonic hydroammonium, ammonium oxalate, ammonium sulfate, the ammonium hydrogen sulfate.

4. hydrocarbon cracking catalyzer according to claim 1 is characterized in that described other modified zeolite is selected from X type zeolite, y-type zeolite, L zeolite, ZSM-5 zeolite, modenite, β zeolite, the omega zeolite modified zeolite that one or more obtain through conventional physics or chemical modification.

5. hydrocarbon cracking catalyzer according to claim 1, the predecessor that it is characterized in that described high-temperature inorganic oxide is selected from one or more in silica-alumina gel, Ludox, aluminium colloidal sol, sial complex sol, the boehmite.

6. hydrocarbon cracking catalyzer according to claim 1 is characterized in that described clay is selected from one or more in kaolin, galapectite, imvite, the sepiolite.

7. hydrocarbon cracking catalyzer according to claim 1, when it is characterized in that described modcfied faujasite prepares, the earth solution of introducing in the exchange slurries is re chloride or rare earth nitrate solution.