A method and system for catalytic cracking of crude oil

Abstract

The present invention relates to a method and system for catalytic cracking of crude oil, the method comprising: S1, introducing a catalytic cracking catalyst into the bottom of a riser reactor, flowing upward under the lifting of a lifting gas, introducing the crude oil after water vapor atomization into a riser reactor to contact the catalytic cracking catalyst for catalytic cracking reaction, and obtaining an oil agent mixed product; S2, performing gas-solid separation on the oil agent mixed product, regenerating the catalytic cracking catalyst to be obtained by gas-solid separation after stripping, and obtaining a regenerated catalytic cracking catalyst with a temperature of 650-750°C; S3, in a reducing atmosphere, performing a reduction reaction on the regenerated catalytic cracking catalyst, and introducing the obtained reduced catalytic cracking catalyst into the riser reactor for recycling. The method of the present invention can effectively increase the temperature of the catalytic cracking reaction system and improve the yield of high-value liquefied gas and gasoline.

Description

Technical Field

[0001] The invention relates to a method and system for catalytic cracking of crude oil. Background Art

[0002] The catalytic cracking unit is the core equipment of the secondary processing of the refinery. It is a process that converts the distillate oil or residual oil obtained from the atmospheric and vacuum tower into fuels such as liquefied gas, gasoline, diesel, or chemical raw materials such as ethylene, propylene, butene, BTX, etc. under the action of catalysts and high temperature. The catalyst is not only the reaction active center of the catalytic cracking reaction, but also the heat and mass transfer carrier of the catalytic cracking regeneration system. The catalyst enters the reactor from the high-temperature regenerator and brings in a large amount of heat, which promotes the occurrence of catalytic cracking reaction. The coke generated by the reaction is loaded on the surface of the catalyst. Then, when entering the regenerator, it burns with oxygen in the air to generate a large amount of heat, completing the transfer and generation of heat.

[0003] With the heavier and inferior processing raw materials and the transformation of oil refining equipment to chemical type, the reaction conditions are more stringent. However, the heat capacity of the catalyst is limited, resulting in limited heat provided to the reaction part, so the reaction temperature is difficult to increase further; at the same time, in order to transfer more heat, the catalyst-to-oil ratio also increases, resulting in more side reactions.

[0004] In the field of catalytic cracking engineering design, the empirical formula used to calculate the heat capacity of catalysts is: Cp (J / (k·g)) = 0.00233 × alumina% + 1.08. Generally, the alumina content is 35-60%, that is, the heat capacity is 1.16-1.22 J / (℃·g). Moreover, the alumina content in conventional catalysts is relatively stable, with small fluctuations, and the increase in heat capacity is limited.

[0005] The heat-generating material releases heat through the continuous redox reaction of metals and their oxides, mainly using the following reactions: 2Cu+O2→2CuO (ΔH=-156KJ / mol=1914J / g), CuO+2H2→Cu+2H2O (ΔH=-95KJ / mol=1190J / g). It can be seen that the heat-generating effect of the heat-generating material is significant. Summary of the invention

[0006] The object of the present invention is to provide a method and system for catalytic cracking of crude oil. The method of the present invention can effectively increase the temperature of the catalytic cracking reaction system.

[0007] In order to achieve the above object, the first aspect of the present invention provides a method for catalytic cracking of crude oil, the method comprising:

[0008] S1, introducing a catalytic cracking catalyst into the bottom of a riser reactor, and allowing the catalyst to flow upward under the lifting of a lifting gas, and introducing the crude oil atomized by water vapor into the riser reactor to contact the crude oil with the catalytic cracking catalyst for a catalytic cracking reaction, thereby obtaining an oil-agent mixed product;

[0009] S2, separating the oil-agent mixed product into gas and solid, and regenerating the spent catalytic cracking catalyst obtained by the gas-solid separation after stripping to obtain a regenerated catalytic cracking catalyst at a temperature of 650-750° C.;

[0010] S3, subjecting the regenerated catalytic cracking catalyst to a reduction reaction in a reducing atmosphere, and introducing the obtained reduced catalytic cracking catalyst into the riser reactor in step S1 for cyclic use;

[0011] Wherein, the catalytic cracking catalyst comprises a catalytic cracking main agent and a catalytic cracking aid. Based on the dry weight of the catalytic cracking aid, the catalytic cracking aid contains 0.1-40 weight % of a copper-containing heating material, 10-60 weight % of an inorganic oxide and the remainder of a carrier; the reduced catalytic cracking catalyst contains the catalytic cracking aid that has been subjected to enhanced reduction.

[0012] Optionally, in step S1, the conditions of the catalytic cracking reaction include: a temperature of 450-650°C, an agent-oil weight ratio of 5-20, a weight ratio of the water vapor to the feed oil of (10-40):100; and a weight ratio of the catalytic cracking aid to the catalytic cracking main agent of 0.01-0.5.

[0013] Optionally, in step S3, the reduction reaction time is 0.5-3 min; the reducing atmosphere contains a reducing gas with a concentration of 15-35% by volume, and the reducing gas is hydrogen and / or dry gas.

[0014] Optionally, in step S2, the gas-solid separation also obtains a mixed oil gas containing dry gas, and the reducing atmosphere contains the dry gas from step S2.

[0015] Optionally, based on the total weight of copper on the surface of the catalytic cracking aid after enhanced reduction, the content of +2-valent copper on the surface of the catalytic cracking aid after enhanced reduction is less than 10 wt%.

[0016] Optionally, the catalytic cracking aid contains 5-35 wt % of a copper-containing heat-generating material, 15-50 wt % of an inorganic oxide and the balance a carrier.

[0017] Optionally, the copper-containing heating material contains one or more of copper, copper oxide and cuprous oxide; the inorganic oxide is selected from alumina and / or silicon oxide; the carrier is selected from one or more of kaolin, halloysite, montmorillonite, diatomaceous earth, attapulgite, sepiolite, halloysite, hydrotalcite, bentonite and rectorite.

[0018] Optionally, the catalytic cracking aid is prepared by a method comprising the following steps: mixing a binder, a carrier and a precursor of a copper-containing heating material, spray drying and calcining;

[0019] The calcination conditions include: a temperature of 500-700°C and a time of 2-5 hours;

[0020] The precursor of the copper-containing heating material is selected from one or more of copper oxide, copper sulfate, copper chloride, copper nitrate and copper carbonate; the binder is selected from one or more of aluminum sol, silica sol, phosphate aluminum sol and peptized pseudo-boehmite.

[0021] The second aspect of the present invention provides a crude oil catalytic cracking system used for the method provided in the first aspect of the present invention, the system comprising: a riser reactor, a gas-solid separation device, a catalyst regenerator and a reduction reactor; the reaction product outlet of the riser reactor is fluidically connected to the inlet of the gas-solid separation device, the solid outlet of the gas-solid separation device is fluidically connected to the catalyst inlet of the catalyst regenerator, the catalyst outlet of the catalyst regenerator is fluidically connected to the solid inlet of the reduction reactor, and the solid outlet of the reduction reactor is fluidically connected to the catalyst inlet of the riser reactor.

[0022] Optionally, the system further comprises a fractionation device, the inlet of the fractionation device is fluidly connected to the gas outlet of the gas-solid separation device, and the dry gas outlet of the fractionation device is fluidly connected to the gas inlet of the reduction reactor.

[0023] Through the above technical scheme, the method of the present invention can effectively increase the reaction temperature of the catalytic cracking reaction system, increase the severity of the reaction, and improve the distribution of the catalytic cracking reaction products.

[0024] Other features and advantages of the present invention will be described in detail in the following detailed description. BRIEF DESCRIPTION OF THE DRAWINGS

[0025] The accompanying drawings are used to provide a further understanding of the present invention and constitute a part of the specification. Together with the following specific embodiments, they are used to explain the present invention but do not constitute a limitation of the present invention. In the accompanying drawings:

[0026] Figure 1 It is a schematic flow diagram of a specific implementation of the system for catalytic cracking of crude oil of the present invention.

[0027] Description of Reference Numerals

[0028] 1. Riser reactor 2. Gas-solid separation device 3. Catalyst regenerator

[0029] 4. Reduction reactor 5. Gas outlet 6. Solid outlet DETAILED DESCRIPTION

[0030] The specific implementation of the present invention is described in detail below in conjunction with the accompanying drawings. It should be understood that the specific implementation described here is only used to illustrate and explain the present invention, and is not used to limit the present invention.

[0031] The first aspect of the present invention provides a method for catalytic cracking of crude oil, the method comprising:

[0032] S1, introducing a catalytic cracking catalyst into the bottom of a riser reactor, and allowing the catalyst to flow upward under the lifting of a lifting gas, and introducing the crude oil atomized by water vapor into the riser reactor to contact the crude oil with the catalytic cracking catalyst for a catalytic cracking reaction, thereby obtaining an oil-agent mixed product;

[0033] S2, separating the oil-agent mixed product into gas and solid, and regenerating the spent catalytic cracking catalyst obtained by the gas-solid separation after stripping to obtain a regenerated catalytic cracking catalyst at a temperature of 650-750° C.;

[0034] S3, subjecting the regenerated catalytic cracking catalyst to a reduction reaction in a reducing atmosphere, and introducing the obtained reduced catalytic cracking catalyst into the riser reactor in step S1 for cyclic use;

[0035] Wherein, the catalytic cracking catalyst comprises a catalytic cracking main agent and a catalytic cracking aid. Based on the dry weight of the catalytic cracking aid, the catalytic cracking aid contains 0.1-40 weight % of a copper-containing heating material, 10-60 weight % of an inorganic oxide and the remainder of a carrier; the reduced catalytic cracking catalyst contains the catalytic cracking aid that has been subjected to enhanced reduction.

[0036] In the method of the present invention, the regenerated catalytic cracking catalyst is subjected to reduction reaction in sequence. Under the condition that the catalyst regeneration temperature is equal, the temperature of the catalyst entering the riser reactor is increased through the reduction reaction, and the copper in the catalyst additive can be reduced to a low-valent form to the maximum extent. When the catalyst is introduced into the riser reactor to participate in the catalytic cracking reaction, the reaction temperature in the riser reactor is increased and the coking problem of the raw material can be reduced, so that the product distribution can be effectively improved, especially the yield of high-value liquefied gas and gasoline can be increased.

[0037] In a specific embodiment of the present invention, in step S1, the conditions of the catalytic cracking reaction include: a temperature of 450-650°C, a catalyst-oil weight ratio of 5-20, a weight ratio of the water vapor to the crude oil of (10-40):100; a weight ratio of the catalytic cracking aid to the catalytic cracking main agent of 0.01-0.5. The catalyst-oil weight ratio refers to the weight ratio of the catalytic cracking catalyst to the crude oil.

[0038] In a specific embodiment of the present invention, in step S3, the reduction reaction time is 0.5-3 min, preferably 1-2.5 min; the reducing atmosphere contains a reducing gas with a concentration of 15-35% by volume, and the reducing gas is hydrogen and / or dry gas.

[0039] In a specific embodiment of the present invention, in step S2, the gas-solid separation also obtains a mixed oil gas containing dry gas, and the reducing atmosphere contains the dry gas from step S2, so as to fully utilize the low-value products of the catalytic cracking reaction without the need to introduce additional foreign materials, which is beneficial to improving the cleanliness, environmental protection and economy of the reaction.

[0040] In a specific embodiment of the present invention, based on the total weight of copper on the surface of the enhanced reduced catalytic cracking aid, the content of +2-valent copper on the surface of the enhanced reduced catalytic cracking aid is less than 10% by weight. When the +2-valent copper on the surface of the enhanced reduced catalytic cracking aid is within the above range, more copper in the surface aid exists in a low-valent reduced state, and the enhanced reduced catalytic cracking aid is used in the catalytic cracking reaction process of crude oil, which can further effectively increase the reaction temperature of catalytic cracking.

[0041] In a specific embodiment of the present invention, the catalytic cracking aid contains 5-35 weight % of copper-containing heat-generating material, 15-50 weight % of inorganic oxide and the balance carrier. More preferably, the catalytic cracking aid contains 10-30 weight % of copper-containing heat-generating material, 15-45 weight % of inorganic oxide and the balance carrier.

[0042] In a specific embodiment of the present invention, the copper-containing heating material contains one or more of copper, copper oxide and cuprous oxide; the inorganic oxide is aluminum oxide and / or silicon oxide; the carrier is selected from one or more of kaolin, halloysite, montmorillonite, diatomaceous earth, attapulgite, sepiolite, halloysite, hydrotalcite, bentonite and rectorite.

[0043] According to the present invention, the catalytic cracking aid can be prepared by a method comprising the following steps: mixing a binder, a carrier and a precursor of a copper-containing heating material, and then spray drying and roasting. Wherein, spray drying and roasting are operations well known to those skilled in the art. In a specific embodiment of the present invention, the roasting conditions include: a temperature of 500-700°C and a time of 2-5 hours. Preferably, the temperature is 520-650°C and the time is 3-5 hours. The roasting can be carried out in equipment conventionally used by those skilled in the art, such as a muffle furnace or a tubular furnace. The present invention does not specifically limit the roasting atmosphere, for example, it can be an air atmosphere or an inert gas atmosphere.

[0044] In a specific embodiment of the present invention, the precursor of the copper-containing heating material is selected from one or more of copper oxide, copper sulfate, copper chloride, copper nitrate and copper carbonate; the binder is selected from one or more of aluminum sol, silica sol, phosphate aluminum sol and peptized pseudo-boehmite.

[0045] The second aspect of the present invention provides a crude oil catalytic cracking system used for the method provided in the first aspect of the present invention, the system comprising: a riser reactor 1, a gas-solid separation device 2, a catalyst regenerator 3 and a reduction reactor 4; the reaction product outlet of the riser reactor 1 is fluidly connected to the inlet of the gas-solid separation device 2, the solid outlet of the gas-solid separation device 2 is fluidly connected to the catalyst inlet of the catalyst regenerator 3, the catalyst outlet of the catalyst regenerator 3 is fluidly connected to the solid inlet of the reduction reactor 4, and the solid outlet of the reduction reactor 4 is fluidly connected to the catalyst inlet of the riser reactor 1.

[0046] The crude oil catalytic cracking system of the present invention comprises a reduction reactor for enhanced reduction of a catalyst promoter. Under the condition that the catalyst regeneration temperature is equal, the temperature of the catalyst entering the riser reactor is increased by the reduction reactor, and the copper in the catalyst promoter can be reduced to a low-valent state to the maximum extent. When the copper is introduced into the riser reactor to participate in the catalytic cracking reaction, the reaction temperature in the riser reactor is increased, the coking problem of the raw material can be reduced, and the yield of high-value liquefied gas and gasoline can be increased.

[0047] In a specific embodiment of the present invention, the system further comprises a fractionation device, the inlet of the fractionation device is fluidly connected to the gas outlet of the gas-solid separation device, and the dry gas outlet of the fractionation device is fluidly connected to the gas inlet of the reduction reactor.

[0048] The present invention is further illustrated by the following examples, but the present invention is not limited thereto.

[0049] The instruments and reagents used in the embodiments of the present invention are all commonly used by those skilled in the art unless otherwise specified. The feedstock oil used in the embodiments is hydrogenated residue oil, and its composition is shown in the following table. The ratio of copper of different valence states on the surface of the catalytic cracking aid to the total amount of copper on the surface is detected by the XPS method.

[0050]

[0051]

[0052] Preparation Examples 1-4 are preparation examples of catalytic cracking aids, wherein Preparation Example 1 is a preparation example of an aid in the prior art, and Preparation Examples 2-4 are catalytic cracking aids prepared by the method of the present invention.

[0053] Preparation Example 1

[0054] The binder, the carrier and the precursor of the copper-containing heating material were mixed according to the proportions in Table 1 to prepare a slurry, and the obtained slurry was spray-dried and then calcined at 650° C. for 4 hours to obtain a catalytic cracking aid containing the copper-containing heating material.

[0055] Table 1

[0056]

[0057]

[0058] Examples 1-3

[0059] In such Figure 1 The catalytic cracking reaction of crude oil is carried out in the industrial simulated catalytic cracking system shown, and the system includes: a riser reactor, a gas-solid separation device, a catalyst regenerator, a reduction reactor and a fractionation device. The reaction product outlet of the riser reactor is fluidly connected to the inlet of the gas-solid separation device, the solid outlet of the gas-solid separation device is fluidly connected to the catalyst inlet of the catalyst regenerator, the catalyst outlet of the catalyst regenerator is fluidly connected to the solid inlet of the reduction reactor, the solid outlet of the reduction reactor is fluidly connected to the catalyst inlet of the riser reactor, the inlet of the fractionation device is fluidly connected to the gas outlet of the gas-solid separation device, and the dry gas outlet of the fractionation device is fluidly connected to the gas inlet of the reduction reactor.

[0060] The following method is used for catalytic cracking of crude oil:

[0061] S1. The catalytic cracking aid prepared in Preparation Example 2-4 is mixed with the catalytic cracking main agent A-1 (purchased from Sinopec Catalyst Company, brand COKC-1) as a catalytic cracking catalyst, wherein the weight ratio of the catalytic cracking aid to the catalytic cracking main agent is 5:95. The catalytic cracking catalyst is introduced into the bottom of the riser reactor, flows upward under the lifting of the lifting gas, and the raw oil atomized by water vapor is introduced into the riser reactor to contact with the catalytic cracking catalyst for catalytic cracking reaction to obtain an oil-agent mixed product. Among them, the weight ratio of water vapor to raw oil is 12:100, the temperature of the catalytic cracking reaction is 530°C, and the weight ratio of agent to oil is 8.

[0062] S2, separating the oil-agent mixture product into gas and solid, and regenerating the spent catalytic cracking catalyst obtained by gas-solid separation after stripping to obtain a regenerated catalytic cracking catalyst at a temperature of 700°C. The separated oil and gas are introduced into a fractionation device for fractionation to obtain dry gas, liquefied gas, gasoline, diesel, and heavy oil, and the dry gas is introduced into step S3 as a reducing gas;

[0063] S3. The regenerated catalytic cracking catalyst is contacted with the dry gas from step S2 to carry out a reduction reaction, and the obtained reduced catalytic cracking catalyst is introduced into a riser reactor for recycling. The reduced catalytic cracking catalyst contains a catalytic cracking aid that has undergone enhanced reduction, and the proportion of surface + divalent copper of the catalytic cracking aid that has undergone enhanced reduction is 1% by weight.

[0064] The reaction temperature change was recorded to examine the heating effect, and the results are shown in Table 2. The results show that after the introduction of the catalytic cracking aid, the reaction temperature increased significantly, but after the content of the copper-containing heating material exceeded 40% by weight, the heating effect increased slowly.

[0065] Example 4

[0066] The catalytic cracking reaction was carried out in the same manner as in Example 1, except that in step S2, dry gas was not introduced into step S3 as reducing gas, and in step S3, 20 volume % hydrogen (the rest being nitrogen) was used as reducing medium.

[0067] The ratio of the surface + divalent copper of the catalytic cracking aid subjected to enhanced reduction contained in the reduced catalytic cracking catalyst was 5% by weight.

[0068] Example 5

[0069] The catalytic cracking reaction was carried out in the same manner as in Example 1, except that in step S1, the weight ratio of water vapor to crude oil was 8:100, the temperature of the catalytic cracking reaction was 530° C., and the catalyst-oil weight ratio was 4.

[0070] Comparative Example 1

[0071] The catalytic cracking reaction was carried out in the same manner as in Example 2, except that step S3 was omitted and the regenerated catalytic cracking catalyst at a temperature of 700° C. was directly introduced into step S1 for recycling.

[0072] Comparative Example 2

[0073] The catalytic cracking reaction of the crude oil was carried out in the same manner as in Example 2, except that the catalytic cracking aid used was Z-1, the temperature variation was shown in Table 2, and the product distribution was shown in Table 3.

[0074] Table 2

[0075]

[0076] Table 3

[0077] Comparative Example 1 Comparative Example 2 Example 1 Example 2 Example 3 Example 4 Example 5 Catalytic cracking additives Z-3 Z-1 Z-2 Z-3 Z-4 Z-2 Z-2 Catalytic cracking agent A-1 A-1 A-1 A-1 A-1 A-1 A-1 Yield, weight % Dry gas 5.27 4.92 4.97 5.00 5.03 4.60 4.31 Liquefied gas 21.62 23.54 24.35 25.04 24.89 24.16 20.32 Coke 11.98 8.60 8.91 9.14 10.19 8.54 11.79 gasoline 22.24 24.12 23.45 23.47 22.49 23.91 21.03 diesel fuel 15.93 16.63 16.10 16.03 16.83 17.18 18.45 Oil slurry 22.96 22.19 22.22 21.32 20.57 21.61 24.1 Conversion rate, weight % 61.11 62.18 61.68 62.65 62.6 61.18 57.45

[0078] As shown in Table 3, it can be found that the high-valent copper heating auxiliary agent in the prior art (Comparative Example 1) significantly increases the coke production, and the yield of high-value liquefied gas and gasoline decreases significantly, and the economic efficiency is poor; the auxiliary agent without copper is used in combination with the main agent as a catalytic cracking catalyst (Comparative Example 2), and the yield of liquefied gas and gasoline is also poor. The catalytic cracking method of the present invention can effectively increase the yield of liquefied gas and gasoline in the product and reduce the output of coke. The method of the present application can effectively improve the product distribution, especially increase the yield of high-value liquefied gas and gasoline.

[0079] The preferred embodiments of the present invention are described in detail above in conjunction with the accompanying drawings. However, the present invention is not limited to the specific details in the above embodiments. Within the technical concept of the present invention, a variety of simple modifications can be made to the technical solution of the present invention, and these simple modifications all belong to the protection scope of the present invention.

[0080] It should also be noted that the various specific technical features described in the above specific embodiments can be combined in any suitable manner without contradiction. In order to avoid unnecessary repetition, the present invention will not further describe various possible combinations.

[0081] In addition, various embodiments of the present invention may be arbitrarily combined, and as long as they do not violate the concept of the present invention, they should also be regarded as the contents disclosed by the present invention.

Claims

1. A method for catalytic cracking of crude oil, the method comprising: S1. Introducing a catalytic cracking catalyst into the bottom of a riser reactor, allowing the catalyst to flow upward under the lifting of a lifting gas, introducing a crude oil atomized by water vapor into the riser reactor to contact the crude oil with the catalytic cracking catalyst for a catalytic cracking reaction, and obtaining an oil-agent mixed product; wherein the conditions of the catalytic cracking reaction include: a temperature of 450-650° C., a catalyst-oil weight ratio of 5-20, a weight ratio of the water vapor to the crude oil of (10-40):100; a weight ratio of the catalytic cracking aid to the catalytic cracking main agent of 0.01-0.5; S2, separating the oil-agent mixed product into gas and solid, and regenerating the spent catalytic cracking catalyst obtained by the gas-solid separation after stripping to obtain a regenerated catalytic cracking catalyst at a temperature of 650-750° C.; S3, subjecting the regenerated catalytic cracking catalyst to a reduction reaction in a reducing atmosphere, and introducing the obtained reduced catalytic cracking catalyst into the riser reactor in step S1 for cyclic use; Wherein, the catalytic cracking catalyst comprises a catalytic cracking main agent and a catalytic cracking aid. Based on the dry weight of the catalytic cracking aid, the catalytic cracking aid contains 5-35 wt % of a copper-containing heating material, 15-50 wt % of an inorganic oxide and the remainder of a carrier; the reduced catalytic cracking catalyst contains the catalytic cracking aid that has been enhanced reduced; based on the total weight of copper on the surface of the catalytic cracking aid that has been enhanced reduced, the content of +2-valent copper on the surface of the catalytic cracking aid that has been enhanced reduced is less than 10 wt %.

2. The method according to claim 1, wherein: In step S3, the reduction reaction time is 0.5-3 min; the reducing atmosphere contains a reducing gas with a concentration of 15-35% by volume, and the reducing gas is hydrogen and / or dry gas.

3. The method according to claim 1, wherein: In step S2, the gas-solid separation also obtains a mixed oil gas containing dry gas, and the reducing atmosphere contains the dry gas from step S2.

4. The method according to claim 1, wherein: The copper-containing heating material contains one or more of copper, copper oxide and cuprous oxide; the inorganic oxide is selected from aluminum oxide and / or silicon oxide; the carrier is selected from one or more of kaolin, montmorillonite, diatomaceous earth, attapulgite, sepiolite, halloysite, hydrotalcite, bentonite and rectorite.

5. The method according to claim 4, wherein: The carrier is halloysite.

6. The method according to claim 1, wherein: The catalytic cracking aid is prepared by a method comprising the following steps: mixing a binder, a carrier and a precursor of a copper-containing heating material, spray drying and calcining; The calcination conditions include: a temperature of 500-700°C and a time of 2-5 hours; The precursor of the copper-containing heating material is selected from one or more of copper oxide, copper sulfate, copper chloride, copper nitrate and copper carbonate; the binder is selected from one or more of aluminum sol, silica sol, phosphate aluminum sol and peptized pseudo-boehmite.

7. A crude oil catalytic cracking system for use in the method according to any one of claims 1 to 6, the system comprising: A riser reactor (1), a gas-solid separation device (2), a catalyst regenerator (3) and a reduction reactor (4); The reaction product outlet of the riser reactor (1) is fluidly connected to the inlet of the gas-solid separation device (2), the solid outlet (6) of the gas-solid separation device (2) is fluidly connected to the catalyst inlet of the catalyst regenerator (3), the catalyst outlet of the catalyst regenerator (3) is fluidly connected to the solid inlet of the reduction reactor (4), and the solid outlet of the reduction reactor (4) is fluidly connected to the catalyst inlet of the riser reactor (1).

8. The system according to claim 7, wherein: The system further comprises a fractionation device, the inlet of the fractionation device being fluidly connected to the gas outlet (5) of the gas-solid separation device (2), and the dry gas outlet of the fractionation device being fluidly connected to the gas inlet of the reduction reactor (4).

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