Modification-catalysis combined method for inferior vacuum residue

Abstract

The invention provides a modification-catalysis combined method for inferior vacuum residue, which comprises the following steps: preheating vacuum residue and water, feeding the preheated vacuum residue and water into a modification reactor for hydrothermal modification, feeding the obtained modified product into a separator to separate out cracked gas, water and modified oil, feeding the modified oil into a catalytic cracking reactor for reaction, separating the obtained reaction oil gas to obtain a product containing a target product; when the target product is gasoline, the reaction temperature of hydrothermal modification is 300-360 DEG C, the reaction pressure is 8-12 MPa, the reaction time is 5-8 min, and the water-oil mass ratio is 1-3; when the target product is liquefied gas, the reaction temperature of hydrothermal modification is 380-420 DEG C, the reaction pressure is 15-20 MPa, the reaction time is 1-4 min, and the water-oil mass ratio is 3-5. The hydrothermal modification can effectively improve the cracking performance of the residual oil in a short time, optimizes the product distribution, and achieves the purpose of high yield of gasoline or liquefied gas, thereby providing a new choice for super-heavy poor-quality oil which is difficult to process by conventional means.

Description

Technical Field

[0001] This invention relates to the field of catalytic cracking technology, specifically to a combined method for upgrading and catalytic cracking of inferior vacuum residue. Background Technology

[0002] The increasing trend towards lower-quality, heavier crude oil has led to a steady rise in the proportion of unconventional crude oil processed. Major oil-producing countries' main oil fields have entered the mid-to-late stages of development, resulting in increasingly lower-quality and heavier crude oil. Unconventional petroleum resources, including heavy crude oil, extra-heavy crude oil, and oil sands bitumen, account for more than two-thirds of the world's proven reserves. These resources have low API gravity and high levels of heteroatoms such as sulfur, nitrogen, and oxygen, as well as high levels of residual carbon, metals, and asphaltenes. In the future, refineries will increasingly rely on lower-quality, heavy crude oil as feedstock. The most significant challenge in processing and utilizing this lower-quality, heavy crude oil is the lightening of vacuum residue. Vacuum residue accounts for 40%–50% of total crude oil. Due to its high density, high residual carbon, high metal content, and high sulfur and nitrogen levels, vacuum residue is very difficult to process. Clean, efficient, and economically feasible vacuum residue processing technology remains one of the key challenges that the refining industry continues to tackle.

[0003] Heavy oil FCC units are the most important production facilities for heavy oil light processing in my country, currently processing approximately 47% of the residue oil. Conventional FCC feedstocks are generally relatively high-quality residue oils with a carbon residue content below 6% and nickel and vanadium content below 35 μg / g. Large quantities of high-sulfur, high-carbon-residue, and high-metal-content residue oils must undergo pretreatment before entering the FCC unit. In the late stages of operation, the demetallization and decarbonization efficiency of the catalyst in the vacuum residue hydrotreating unit decreases. During catalyst replacement in the hydrotreating unit, the upgrading of vacuum residue becomes a limiting factor for its entry into catalytic cracking. Improving the processing performance of vacuum residue using simple and effective methods has become a crucial technical means urgently needed by refineries.

[0004] Supercritical water (SCW) is a preferred solvent due to its unique physicochemical properties, being inexpensive, readily available, and environmentally friendly, and is widely used in research on heavy oil reforming. CN101558136A discloses a method for reforming heavy oil using supercritical water. This method allows for the continuous reforming of heavy oil into a light oil with low density, low viscosity, and low carbon residue using a tubular reactor through three or more processes: mixing, reforming, and separation. While this method can reform heavy oil, it does not address the compatibility with feedstocks, the degree of product reforming, or how the reformed product can be processed and utilized.

[0005] CN101942338A discloses a combined process for heavy oil reforming. Heavy oil is mixed with a hydrogen-donating solvent such as tetrahydronaphthalene or decahydronaphthalene and reformed under supercritical conditions. The reformed product, after separating coke and light fractions, is then processed into a heavy oil fraction via catalytic cracking to produce dry gas, liquefied petroleum gas (LPG), etc. Water can be introduced during the supercritical treatment. However, this method is a hydrotreating process using mixed water, not using water as the primary solvent, and coke is generated during supercritical treatment. Furthermore, no correlation has been established between the supercritical reforming conditions and the target products of catalytic cracking.

[0006] With the development and changes in the market, the efficient processing of vacuum residue has become an essential technical requirement for refining and chemical enterprises to reduce raw material costs. At the same time, catalytic cracking to adapt to market changes and flexibly produce liquefied gas or gasoline has also become an urgent technical requirement.

[0007] Optimizing the supercritical reforming conditions of vacuum residue to match the target product structure of catalytic cracking is a technical problem that urgently needs to be solved. Summary of the Invention

[0008] To address the above problems, this invention provides a combined method for upgrading and catalytic oxidation of inferior vacuum residue.

[0009] This invention provides a combined method for upgrading and catalytic oxidation of inferior vacuum residue, comprising:

[0010] The vacuum residue and water are preheated and then fed into a reforming reactor for hydrothermal reforming. The resulting reformed product is fed into a separator to separate cracked gas, water and reformed oil. The reformed oil is then fed into a catalytic cracking reactor for reaction. The resulting reaction oil and gas are separated to obtain a product including the target product.

[0011] The following conditions are used to control hydrothermal reforming:

[0012] When the target product is gasoline, the hydrothermal reforming reaction temperature is 300–360℃, the reaction pressure is 8–12 MPa, the reaction time is 5–8 min, and the water-to-oil mass ratio is 1–3; or,

[0013] When the target product is liquefied petroleum gas (LPG), the hydrothermal reforming reaction temperature is 380–420℃, the reaction pressure is 15–20 MPa, the reaction time is 1–4 min, and the water-oil mass ratio is 3–5.

[0014] Optionally, the vacuum residue oil has a density greater than 930 kg / m³ at 20°C. 3 The residual carbon content is not less than 5%, and the total mass fraction of resin and asphalt is greater than 20%.

[0015] Optionally, the preheating temperature of vacuum residue and water is 250–300°C respectively.

[0016] Optionally, the reforming reactor is an upward-flowing tubular reactor, preferably an upward-flowing vertical tubular reactor.

[0017] Optionally, the yield of solid coke in the modified product is 0.

[0018] Optionally, the temperature of the separator is 250–300°C and the pressure is 0.1–0.3 MPa.

[0019] Optionally, the water content in the modified oil is 0.1% to 0.3% by mass.

[0020] Optionally, the modified oil may be mixed with one or more of the following: recycled oil, recycle oil, and catalytic cracking feedstock, and then fed into a catalytic cracking reactor for reaction.

[0021] Optionally, the catalytic cracking reactor is selected from one or more of the following: riser reactor, fluidized bed reactor, and upward conveyor reactor, or a combination of multiple reactors of the same type mentioned above, including parallel and / or series connections; wherein, the riser reactor is a variable diameter or constant diameter riser, and the fluidized bed reactor is one or more of the following: variable diameter or constant diameter fast bed reactor, conveyor bed reactor, and dense phase fluidized bed reactor.

[0022] Optionally, the density of the catalyst in the catalytic cracking reactor is 50–150 kg / m³. 3 .

[0023] Beneficial effects:

[0024] This invention employs hydrothermal conditions for oil refining, achieving similar refining effects in a shorter time compared to viscosity-reducing cracking, effectively improving processing efficiency. Furthermore, the selected conditions result in no coke formation, simplifying the process and facilitating implementation. Hydrothermal refining can effectively improve the cracking performance of residual oil and optimize product distribution within a short period, achieving the goal of producing more gasoline or liquefied petroleum gas. This provides a new option for processing ultra-heavy, low-quality oils that are difficult to process using conventional methods. Attached Figure Description

[0025] Figure 1 This is a schematic flowchart of the method for upgrading and catalytically combining inferior vacuum residue oil according to the present invention. Detailed Implementation

[0026] The present application will now be described in further detail with reference to the accompanying drawings and embodiments. Through these descriptions, the features and advantages of the present application will become clearer and more apparent.

[0027] The term “exemplary” as used herein means “serving as an example, embodiment, or illustration.” Any embodiment illustrated herein as “exemplary” is not necessarily to be construed as superior to or better than other embodiments. Although various aspects of embodiments are shown in the accompanying drawings, the drawings are not necessarily drawn to scale unless specifically indicated otherwise.

[0028] Furthermore, the technical features involved in the different embodiments of this application described below can be combined with each other as long as they do not conflict with each other.

[0029] This invention provides a combined method for upgrading and catalytic oxidation of inferior vacuum residue, comprising:

[0030] The vacuum residue and water are preheated and then fed into a reforming reactor for hydrothermal reforming. The resulting reformed product is fed into a separator to separate cracked gas, water and reformed oil. The reformed oil is then fed into a catalytic cracking reactor for reaction. The resulting reaction oil and gas are separated to obtain a product including the target product.

[0031] The following conditions are used to control hydrothermal reforming:

[0032] When the target product is gasoline, the hydrothermal reforming reaction temperature is 300–360℃, the reaction pressure is 8–12 MPa, the reaction time is 5–8 min, and the water-to-oil mass ratio is 1–3; or,

[0033] When the target product is liquefied petroleum gas (LPG), the hydrothermal reforming reaction temperature is 380–420℃, the reaction pressure is 15–20 MPa, the reaction time is 1–4 min, and the water-oil mass ratio is 3–5.

[0034] The favorable mass transfer and diffusion conditions provided by SCW (Self-Cracking Weakness) facilitate the decomposition of heavy oil components into lighter components. However, once cracking reaches a certain depth, condensation gradually becomes dominant in the reaction process. To improve the thermal cracking of heavy oil using the superior phase structure and diffusion environment provided by SCW, the reaction time, or cracking depth, must be controlled within a certain range. Otherwise, improvements in the diffusion environment will inevitably and simultaneously accelerate condensation significantly in the later stages of cracking.

[0035] The increase in reaction temperature promotes the evolution of the residue oil and water mixture from an emulsion structure to a pseudo-homogeneous structure. Hydrocarbon molecules with lower carbon numbers continuously dissolve from the oil droplets into the SCW phase, while the number of high-boiling-point and high-carbon-number hydrocarbon molecules remaining in the oil droplets decreases. As most of the relatively light hydrocarbons dissolve into the aqueous phase, the original colloidal structure of the heavy components in the oil droplets is eventually destroyed and dispersed in the SCW phase in the form of coke-like aggregates.

[0036] Based on the above research, it is necessary to control appropriate temperature, time, and pressure conditions to achieve a better upgrading effect on the vacuum residue oil, thus facilitating the formation of the target product, while avoiding over-cracking and condensation coking to prevent the formation of coke. The upgrading-catalytic combination method for inferior vacuum residue oil of this invention can be carried out according to... Figure 1 The process is as shown. After preheating, vacuum residue and water enter the reforming reactor for hydrothermal reforming. The resulting reformed product enters the separator to separate gas and reformed oil. Further separation of the gas yields cracked gas and water. The water separated by condensation can be recycled. The separated reformed oil enters the catalytic cracking unit for reaction under appropriate process conditions. The resulting reaction oil and gas can be separated to obtain products such as liquefied petroleum gas and gasoline. The resulting spent catalyst can be recycled after regeneration.

[0037] Through long-term research and experimentation, the inventors of this application unexpectedly discovered that, after preheating vacuum residue and water, hydrothermal reforming is performed. The reformed product is then separated into cracked gas and water. When the resulting reformed oil undergoes catalytic cracking, to maximize gasoline production (i.e., the target product is gasoline), the reaction temperature of the hydrothermal reforming is controlled at 300–360°C, the reaction pressure at 8–12 MPa, the reaction time at 5–8 min, and the water-to-oil mass ratio at 1–3. Under these conditions, the reformed oil undergoing catalytic cracking can significantly increase the gasoline yield. Similarly, to maximize liquefied petroleum gas (LPG) production (i.e., the target product is LPG), the reaction temperature of the hydrothermal reforming is controlled at 380–420°C, the reaction pressure at 15–20 MPa, the reaction time at 1–4 min, and the water-to-oil mass ratio at 3–5. Under these conditions, the reformed oil undergoing catalytic cracking can significantly increase the LPG yield. Hydrothermal reforming of vacuum residue and water under optimized reaction conditions is beneficial for catalytic cracking to produce more target products such as gasoline or liquefied petroleum gas, enabling more targeted production. This method establishes the correlation between hydrothermal reforming conditions and catalytic cracking products, and can effectively improve reforming efficiency, increase vacuum residue conversion rate and high-value product yield. Furthermore, this non-hydrogen-dependent inferior vacuum residue reforming-catalytic combination method significantly reduces the amount of coke generated.

[0038] In one embodiment of the aforementioned method for upgrading and catalytically reacting inferior vacuum residue of the present invention, the vacuum residue has a density greater than 930 kg / m³ at 20°C. 3 The residual carbon content is not less than 5%, and the total mass fraction of resin and asphalt is greater than 20%.

[0039] It should be noted that the vacuum residue can be a vacuum residue fraction obtained under conventional vacuum distillation conditions well known in the art. Selecting vacuum residue that meets the above conditions and performing reforming and catalytic cracking according to the reforming-catalytic combination method of the present invention can better produce the target product gasoline or liquefied petroleum gas.

[0040] In another embodiment of the method for upgrading and catalytically combining inferior vacuum residue of the present invention, the preheating temperature of vacuum residue and water is 250-300°C respectively.

[0041] Specifically, vacuum residue and water can be preheated separately before entering the reforming reactor. By controlling the preheating temperature of vacuum residue and water as described above, this preheating helps to improve the reforming rate and effect of vacuum residue and water. The reformed oil obtained through hydrothermal reforming can generate gasoline and liquefied petroleum gas at a higher yield during catalytic cracking.

[0042] In one embodiment of the aforementioned method for upgrading and catalytically combining inferior vacuum residue of the present invention, the upgrading reactor is an upward-flowing tubular reactor, preferably an upward-flowing vertical tubular reactor.

[0043] As a preferred embodiment, the modified oil is hydrothermally reformed in an upward-flowing vertical reactor under the above conditions. The resulting modified oil is then subjected to a subsequent catalytic cracking reaction, which can significantly reduce coke production while greatly increasing the yield of the target product, gasoline or liquefied petroleum gas.

[0044] In one embodiment of the aforementioned method for upgrading and catalytically combining inferior vacuum residue of the present invention, the yield of solid coke in the upgraded product is 0.

[0045] In the reforming-catalytic combination method of the present invention, the hydrothermal reforming process is carried out under the above conditions, the generation of solid coke in the reforming product is controlled, and the reformed oil obtained by separating the reforming product with a solid coke yield of 0 is used as the feedstock for catalytic cracking. This can complete the catalytic cracking reaction with a higher target product yield, and in particular, can further reduce the generation of coke.

[0046] In one embodiment of the aforementioned method for upgrading and catalytically combining inferior vacuum residue oil of the present invention, the temperature of the separator is 250-300°C and the pressure is 0.1-0.3 MPa.

[0047] In one embodiment of the aforementioned method for upgrading and catalytically combining inferior vacuum residue of the present invention, the water mass fraction in the upgraded oil is 0.1-0.3%.

[0048] It should be noted that by controlling the temperature and pressure of the modified products in the separator as described above, and by controlling the mass fraction of water in the modified oil as described above, the modified oil can generate more of the target product gasoline or liquefied petroleum gas through catalytic cracking reaction, and the amount of coke generated is reduced.

[0049] In one embodiment of the aforementioned method for upgrading and catalytically reacting inferior vacuum residue of the present invention, the upgraded oil is optionally mixed with one or more of circulating oil, recycle oil, and catalytic cracking feedstock before being fed into a catalytic cracking reactor for reaction.

[0050] Modified oil can be processed as a feedstock for catalytic cracking on its own, or it can be mixed with one or more of the following: recycled oil, recycle oil, and catalytic cracking feedstock. It is preferable to process it after mixing it with catalytic cracking feedstock.

[0051] In one embodiment of the aforementioned method for upgrading and catalytically combining inferior vacuum residue of the present invention, the catalytic cracking reactor is selected from one or more of the following: riser reactor, fluidized bed reactor, and upward conveyor reactor, or a combination of multiple reactors of the same type, including parallel and / or series connections; wherein, the riser reactor is a variable diameter or constant diameter riser, and the fluidized bed reactor is one or more of the following: variable diameter or constant diameter fast bed reactor, conveyor bed reactor, and dense phase fluidized bed reactor.

[0052] Specifically, when the catalytic cracking reactor is a combination of multiple reactors of the same type, it can be a combination of two or more. In the reforming-catalytic combination method of the present invention, the reformed oil obtained through hydrothermal reforming and separation can undergo catalytic cracking reaction well in the aforementioned catalytic cracking reactor, achieving a high yield of the target product.

[0053] In one embodiment of the aforementioned method for upgrading and catalytically combining inferior vacuum residue of the present invention, the density of the catalyst in the catalytic cracking reactor is 50–150 kg / m³. 3 .

[0054] For different target products, catalytic cracking can be carried out using appropriate processes. When gasoline is the target product, conventional catalytic cracking processes and catalysts can be selected, such as riser catalytic cracking, dual riser catalytic cracking, and variable diameter riser catalytic cracking. When liquefied petroleum gas (LPG) is the main target product, conventional catalytic cracking processes and catalysts can be selected. When the target product is gasoline or LPG, the conditions for the cracking / cracking reaction can include: a reaction temperature of 500–600℃, a catalyst-to-oil weight ratio of 6–20, a water-to-oil weight ratio of 0.05–0.3, and a space velocity of 2–10 h⁻¹. -1 Preferably, based on the fundamental properties of vacuum residue—high density, high viscosity, high carbon residue, and high metal content—the catalyst density in the reactor of the corresponding process is 20% to 50% higher than that of conventional processes. This promotes the gasification of heavy oil feedstock and provides more acidic centers to facilitate cracking / pyrolysis reactions, thereby further increasing the yield of the target product and reducing coke formation.

[0055] The present invention will be further described in detail below through examples, but these examples are not intended to limit the invention. In the following examples, unless otherwise specified, the experimental instruments and raw materials involved are all commercially available products.

[0056] To fully demonstrate the reactivity of the reformed vacuum residue, the catalytic unit employed the same process conditions and catalyst to highlight the differences in the target products. The properties of the heavy oil feedstock used in the examples are shown in Table 1. The commercial brand of the cracking catalyst used was CDOS, produced by Qilu Catalyst Plant, Catalyst Division of China Petroleum & Chemical Corporation (Sinopec). The catalyst properties are shown in Table 2.

[0057] Table 1 Properties of Heavy Oil Feedstock

[0058]

[0059] Table 2 Catalyst Properties

[0060]

[0061]

[0062] Example 1

[0063] According to the embodiments Figure 1 The process was tested on a medium-sized unit. Vacuum residue and water were preheated to 280°C. Hydrothermal reforming was carried out in a reforming reactor at a reaction temperature of 340°C, a water-to-oil mass ratio of 2, a reaction pressure of 10 MPa, and a reaction time of 6 min. The reformed product (0% solid coke yield) entered a separator where gases (cracked gas and water) were separated at a temperature of 260°C and a pressure of 0.2 MPa. The resulting reformed oil (0.15% water by mass) entered the catalytic cracking unit. The reaction was carried out at a reaction temperature of 520°C and a space velocity of 4 h⁻¹. -1 The catalyst-to-oil weight ratio is 8, the water-to-oil weight ratio is 0.1, and the catalyst density per unit volume in the reactor is 70 kg / m³. 3 The reaction proceeds under specific conditions, and the reacted oil and gas are then separated to obtain the final product. The reforming reactor is an upflow riser reactor. The catalytic cracking reactor in the catalytic cracking unit is a riser reactor. Detailed operating conditions and experimental results are shown in Table 3.

[0064] Example 2

[0065] According to the embodiments Figure 1 The process was tested on a medium-sized unit. Vacuum residue and water were preheated to 280°C. Hydrothermal reforming was carried out in a reforming reactor at a reaction temperature of 390°C, a water-to-oil mass ratio of 4, a reaction pressure of 17 MPa, and a reaction time of 2 min. The reformed product (0% solid coke yield) entered a separator where gases (cracked gas and water) were separated at 260°C and 0.2 MPa. The resulting reformed oil (0.12% water by mass) entered the catalytic cracking unit. The reaction was carried out at a reaction temperature of 520°C and a space velocity of 4 h⁻¹. -1The catalyst-to-oil weight ratio is 8, the water-to-oil weight ratio is 0.1, and the catalyst density per unit volume in the reactor is 70 kg / m³. 3 The reaction proceeds under specific conditions, and the reacted oil and gas are then separated to obtain the final product. The reforming reactor is an upflow riser reactor. The catalytic cracking reactor in the catalytic cracking unit is a riser reactor. Detailed operating conditions and experimental results are shown in Table 3.

[0066] Comparative Example 1

[0067] The reaction conditions of the catalytic unit in the experimental apparatus were the same as in Example 1, without the modification unit. Detailed operating conditions and experimental results are shown in Table 3.

[0068] Comparative Example 2

[0069] The reaction conditions of the catalytic unit in the experimental apparatus were the same as in Example 1, with the modified oil of vacuum residue heat-treated at 390°C for 40 min used as the catalytic feedstock. Detailed operating conditions and experimental results are shown in Table 3.

[0070] Table 3

[0071] Reaction medium Comparative Example 1 Comparative Example 2 Example 1 Example 2 Upgrading temperature / °C / 390 340 390 Water to oil mass ratio / / 2 4 Reaction pressure / MPa / 1 10 17 Upgrading time / min / 40 6 2 Product distribution / % Liquefied gas 5.03 13.68 15.01 18.19 Propylene 1.80 4.51 4.91 6.18 Gasoline 29.83 29.54 32.85 31.00 Coke 18.83 16.27 14.74 14.48

[0072] As shown in Table 3, compared with the untreated and heat-treated vacuum residue, the hydrothermally reformed vacuum residue yielded more high-value products and reduced the amount of coke generated by catalytic cracking. The separator separation conditions and catalytic cracking reaction conditions were the same in Examples 1 and 2. The hydrothermal reforming conditions of vacuum residue were cleverly controlled in Examples 1 and 2. Example 1 achieved a higher gasoline production, while Example 2 achieved a higher LPG production.

[0073] In the description of this application, it should be noted that the terms "upper", "lower", "inner", "outer", "front", "rear", "left", "right", etc., indicate the orientation or positional relationship based on the orientation or positional relationship in the working state of this application. They are only for the convenience of describing this application and simplifying the description, and do not indicate or imply that the device or element referred to must have a specific orientation, or be constructed and operated in a specific orientation. Therefore, they should not be construed as limitations on this application.

[0074] In the description of this application, it should be noted that, unless otherwise expressly specified and limited, the terms "installation," "connection," and "linking" should be interpreted broadly. Those skilled in the art can understand the specific meaning of these terms in this application based on the specific circumstances.

[0075] The present application has been described above with reference to preferred embodiments; however, these embodiments are merely exemplary and illustrative. Various substitutions and modifications can be made to the present application based on these embodiments, all of which fall within the protection scope of the present application.

Claims

1. A combined method for upgrading and catalytic modification of inferior vacuum residue, characterized in that, include: The vacuum residue and water are preheated and then fed into a reforming reactor for hydrothermal reforming. The resulting reformed product is fed into a separator to separate cracked gas, water and reformed oil. The reformed oil is then fed into a catalytic cracking reactor for reaction. The resulting reaction oil and gas are separated to obtain a product including the target product. The following conditions are used to control hydrothermal reforming: When the target product is gasoline, the hydrothermal reforming reaction temperature is 300–360℃, the reaction pressure is 8–12 MPa, the reaction time is 5–8 min, and the water-to-oil mass ratio is 1–3; or, When the target product is liquefied petroleum gas (LPG), the hydrothermal reforming reaction temperature is 380–420℃, the reaction pressure is 15–20 MPa, the reaction time is 1–4 min, and the water-oil mass ratio is 3–5.

2. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The vacuum residue oil has a density greater than 930 kg / m³ at 20°C. 3 The residual carbon content is not less than 5%, and the total mass fraction of resin and asphalt is greater than 20%.

3. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The preheating temperatures for vacuum residue and water are 250–300°C respectively.

4. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The reforming reactor is an upward-flowing tubular reactor, preferably an upward-flowing vertical tubular reactor.

5. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The yield of solid coke in the modified product is 0.

6. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The temperature of the separator is 250–300℃ and the pressure is 0.1–0.3 MPa.

7. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The modified oil contains 0.1% to 0.3% water by mass.

8. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The modified oil is optionally mixed with one or more of the following: recycled oil, recycle oil, and catalytic cracking feedstock, and then fed into a catalytic cracking reactor for reaction.

9. The method for upgrading and catalytically reacting inferior vacuum residue oil according to claim 1, characterized in that, The catalytic cracking reactor is selected from one or more of the following: riser reactor, fluidized bed reactor, and upward conveyor reactor, or a combination of multiple reactors of the same type mentioned above, including parallel and / or series connections; wherein, the riser reactor is a variable diameter or constant diameter riser, and the fluidized bed reactor is one or more of the following: variable diameter or constant diameter fast bed reactor, conveyor bed reactor, and dense phase fluidized bed reactor.

10. The method for upgrading and catalytically combining inferior vacuum residue oil according to claim 1, characterized in that, The density of the catalyst in the catalytic cracking reactor is 50–150 kg / m³. 3 .

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