CN102344828B - Processing method of inferior residual oil - Google Patents

Abstract

A method for processing inferior residual oil. The present invention is a combined method of residual oil hydrogenation, catalytic cracking heavy oil hydrogenation and catalytic cracking. The hydrogenated residual oil is used as the raw material of the catalytic cracking unit, and the catalytic cracking heavy oil obtained by catalytic cracking is divided into two parts, and one part is used as the dilution of the residual oil raw material. The oil enters the residual oil hydrogenation reactor, and the other part undergoes separate hydrogenation and enters the catalytic cracking heavy oil hydrogenation reactor. The invention not only achieves the purpose of reducing the viscosity of residual oil raw materials and promoting the hydrogenation and de-impurity reaction of residual oil, but also realizes the separate hydrofining of catalytic cracking heavy oil, avoiding the heavy metals such as Ni and V in the residual oil, and the residual carbon value and The influence of asphaltenes can saturate most of the polycyclic aromatic hydrocarbons in the catalytic cracking heavy oil, improve its cracking performance, and significantly increase the liquid yield of the catalytic cracking unit.

Description

A kind of processing method of inferior residual oil

technical field

The invention belongs to a method for processing hydrocarbon oil, in particular to a combination of a method for refining hydrocarbon oil in the presence of hydrogen and a method for cracking hydrocarbon oil in the absence of hydrogen.

Background technique

Petroleum is a non-renewable energy source. my country's imported crude oil is showing a rapid growth trend. In recent years, the price of crude oil has been rising. Benefits are also of great significance to my country's energy security.

The combination of residual oil hydrogenation and catalytic cracking technology is a residual oil deep processing technology that can deeply convert residual oil and achieve clean production. However, the traditional residual oil hydrogenation-catalytic cracking combination technology is a one-way combination, that is, the residual oil is used as a catalytic cracking raw material after hydrogenation, and the catalytic cracking heavy oil circulates itself in the catalytic cracking unit. The disadvantages of this process are: (1) for catalytic cracking, because catalytic cracking heavy oil contains a large amount of polycyclic aromatic hydrocarbons, the self-circulation in the catalytic cracking unit leads to low yield of light oil and large amount of coke, which reduces the processing capacity of RFCC unit and Economic benefits; (2) For residual oil hydrogenation units, residual oil hydrogenation is a diffusion-controlled reaction, and high-viscosity residual oil will reduce the diffusion and reaction performance, and increase the tendency of catalyst coking and deactivation; but if a large amount of straight-run wax oil is used If it is used as diluent oil, it faces the problem of competing for raw materials with the hydrocracking unit that produces ethylene raw materials.

CN1382776A discloses a combined method of residual oil hydrotreating and heavy oil catalytic cracking. In this method, residual oil, oil slurry distillate, catalytic cracking heavy cycle oil, and optional distillate oil are put into a hydrotreating unit together, and hydrogenation reaction is carried out in the presence of hydrogen and a hydrogenation catalyst; the resulting oil obtained from the reaction is distilled After gasoline and diesel are produced, the hydrogenated residual oil enters the catalytic cracking unit together with the optional vacuum gas oil, and undergoes cracking reaction in the presence of a cracking catalyst; the heavy cycle oil obtained from the reaction enters the residual oil hydrogenation unit. In the method, the catalytic cracking heavy cycle oil is mixed into the residual oil hydrogenation raw material, which can reduce the viscosity of the residual oil, improve the compatibility of the residual oil system, and thus can promote the hydrogenation and removal of impurities of the residual oil. For catalytic cracking, the catalytic cracking heavy cycle oil rich in a large amount of polycyclic aromatic hydrocarbons can be hydrogenated together with the residual oil in the residual oil hydrogenation unit to increase its hydrogen content and saturation, and then return to the catalytic cracking unit for cracking, light The oil yield increases and the coke yield decreases.

Contents of the invention

The purpose of the present invention is to provide a processing method of inferior residual oil on the basis of the prior art, through the combination method of residual oil hydrotreating, catalytic cracking heavy oil hydrogenation and catalytic cracking, so as to convert inferior residual oil to the maximum extent For light oil.

In the prior art, there is a technical solution for recycling catalytic cracked heavy oil to a residual oil hydrogenation unit. However, the inventors have found through research that adding a small amount of catalytically cracked heavy oil into the residual oil feed can reduce the viscosity of the residual oil feed and promote the impurity removal reaction of the residual oil. However, with the increase of the blending ratio of catalytic cracking heavy oil, when the viscosity of the feedstock of the residual oil hydrogenation unit decreases to a certain level, the blending ratio of catalytic cracking heavy oil will continue to increase, and the promotion effect on the reaction of residual oil hydrogenation to remove impurities will be no longer increase. At the same time, because the residual oil contains a large amount of heavy metals such as Ni and V, the residual carbon value is high, and the asphaltene is high, which will seriously affect the hydrogenation effect of catalytic cracking heavy oil. Therefore, the present invention divides catalytic cracking heavy oil into two parts, one part is used as the dilution oil of residual oil raw material, and the other part is subjected to separate hydrotreating. In this way, the viscosity of residual oil raw materials can be reduced, and the purpose of promoting the hydrogenation and impurity removal reaction of residual oil can be achieved. At the same time, the separate hydrofining of catalytic cracking heavy oil can be realized, and the accumulation of heavy metals such as Ni and V, residual carbon and asphaltenes in residual oil can be avoided. Influence, improve the effect of catalytic cracking heavy oil hydrogenation.

The provided method of the present invention comprises:

(1) The residual oil raw material, part of the catalytically cracked heavy oil from step (2) and hydrogen enter the residual oil hydrogenation reactor together, and react under the action of the residual oil hydrogenation catalyst, and the reactant flow enters the high-pressure separator to be separated into a gas phase Logistics and liquid phase logistics, wherein the gas phase stream is recycled after being purified and boosted, and the liquid phase stream is fractionated to obtain gas, hydrogenated gasoline, hydrogenated diesel oil and hydrogenated residue;

(2), step (1) obtained hydrogenated residue enters the catalytic cracking unit, reacts in the presence of a catalytic conversion catalyst, and separates the reaction product to obtain dry gas, liquefied gas, catalytic cracked gasoline, catalytic cracked diesel oil and catalytic cracked heavy oil;

(3) The catalytic cracking heavy oil obtained in step (2) is divided into two parts, one part is returned to step (1) and mixed with residual oil raw material to enter the residual oil hydrogenation reactor, and the remaining part is mixed with hydrogen to enter the catalytic cracking heavy oil hydrogenation reaction The reaction is carried out under the action of the catalytic cracking heavy oil hydrogenation catalyst, and the reactant flow enters the high-pressure separator described in step (1) for gas-liquid separation.

The residual oil raw material described in step (1) is atmospheric residual oil and/or vacuum residual oil, the viscosity is between 500mm ² /s-3000mm ² /s, and the viscosity mentioned refers to kinematic viscosity (100°C) .

The reaction conditions of the residual oil hydrogenation reactor are: hydrogen partial pressure 5.0MPa-22.0MPa, reaction temperature 330°C-450°C, volume space velocity 0.1h ^-1 -3.0h ^-1 , volume ratio of hydrogen to raw oil (hydrogen Oil volume ratio) 350-2000. Described catalyst can be various existing residual oil hydrogenation catalysts, and its active metal component is nickel-tungsten, nickel-tungsten-cobalt, nickel-molybdenum or cobalt-molybdenum, and carrier is alumina, silicon dioxide or Amorphous silica-alumina, among which alumina is the most commonly used carrier. The type of residual oil hydrogenation reactor can be fixed bed, moving bed or ebullating bed, and the residual oil hydrogenation unit includes at least one reactor and one fractionation tower.

The hydrogenated residual oil preheated in step (2) enters the first reaction zone of the catalytic conversion reactor under the lifting effect of water vapor to contact with the hot regenerated catalytic conversion catalyst. 0.05 seconds-1.0 seconds, the weight ratio of catalyst to feedstock oil (hereinafter referred to as agent-oil ratio) is 3-15:1, the weight ratio of water vapor to feedstock oil (hereinafter referred to as water-oil ratio) is 0.03-0.3:1, Under the condition of pressure of 130kPa-450kPa, macromolecule cracking reaction occurs, and at least one impurity in metal, sulfur, and nitrogen in inferior raw material oil is removed; the generated oil gas and the catalyst used in the first reaction zone enter the second stage of the catalytic conversion reactor In the second reaction zone, the cracking reaction, hydrogen transfer reaction and isomerization reaction are carried out under the conditions of the reaction temperature of 420°C-550°C and the reaction time of 1.5 seconds to 20 seconds; the reaction products are separated to obtain dry gas, propylene, propane, C4 Hydrocarbons, FCC gasoline, FCC diesel and FCC heavy oil.

The distillation range of catalytic cracking gasoline or catalytic cracking diesel oil described in step (2) is adjusted according to actual needs, not limited to full range gasoline or diesel oil.

The catalytic conversion catalyst described in step (2) comprises zeolite, inorganic oxide and optional clay, and each component accounts for the total weight of the catalyst respectively: zeolite 1%-50% by weight, inorganic oxide 5%-99% by weight %, clay 0%-70% by weight. Wherein the zeolite as an active component is selected from medium-pore zeolite and/or optional large-pore zeolite, medium-pore zeolite accounts for 0%-100% by weight of the total weight of zeolite, preferably 20%-80% by weight, large-pore zeolite It accounts for 0% to 100% by weight of the total weight of the zeolite, preferably 20% to 80% by weight. The medium-pore zeolite is selected from ZSM series zeolite and/or ZRP zeolite, and the above-mentioned medium-pore zeolite can also be modified with non-metal elements such as phosphorus and/or transition metal elements such as iron, cobalt, and nickel. ZSM series zeolites are selected from one or more mixtures of ZSM-5, ZSM-11, ZSM-12, ZSM-23, ZSM-35, ZSM-38, ZSM-48 and other similar structure zeolites, For a more detailed description of ZSM-5 see US 3,702,886. The large-pore zeolite is selected from one or more mixtures of zeolites in the group consisting of rare earth Y (REY), rare earth hydrogen Y (REHY), ultrastable Y obtained by different methods, and high silicon Y.

The distillation range of the catalytic cracking heavy oil obtained in the step (2) is 260°C-550°C, and the weight percentage of the catalytic cracking heavy oil is 12%-60% based on the catalytic cracking fresh raw material. Preferably 15%-40%.

In step (1), based on the residual oil raw material, catalytically cracked heavy oil is used as the diluent oil of the residual oil raw material, and the blending ratio is 5% to 20% by weight, and the specific ratio is determined by the viscosity of the residual oil raw material. The viscosity of the residual oil raw material after being mixed with catalytic cracking heavy oil is controlled to be 50mm ² /s-300mm ² /s, preferably 100mm ² /s-200mm ² /s, and the said viscosity refers to kinematic viscosity (100°C). The rest of the catalytic cracking heavy oil is mixed with hydrogen and then enters the catalytic cracking heavy oil hydrogenation reactor.

The catalytic cracking heavy oil hydrogenation catalyst described in step (3) includes a hydrogenation protecting agent, a hydrogenation deasphaltene agent, and a hydrofinishing agent in sequence according to the flow direction of the reactant stream, and is based on the volume of the overall catalytic cracking heavy oil hydrogenation catalyst. The filling volume percentages of the hydrogenation protecting agent, hydrogenation deasphaltene agent and hydrofinishing agent are respectively 2%-30%, 5%-50% and 5%-93%.

The hydrogenation protecting agent described in the step (3) is a Raschig ring, containing a kind of alumina carrier and molybdenum and/or tungsten loaded on the alumina carrier, and nickel and/or cobalt, with the total amount of the catalyst Based on weight and calculated as oxides, the content of molybdenum and/or tungsten is 1-10% by weight, and the content of nickel and/or cobalt is 0.5-3% by weight. The alumina is γ-alumina. The pore volume of the hydrogenation protecting agent is not less than 0.50ml/g, preferably not less than 0.60ml/g. The hydrogenation protecting agent has low carbon deposition, low pore volume decrease rate, good activity stability and high strength. The present invention fills the upper part of the reactor with a hydrogenation protective agent with a large void ratio, which can further remove the fine catalytic cracking catalyst powder entrained in the raw material, and at the same time effectively remove the fouling substances that are prone to coke in the raw material to achieve protection. The purpose of the main catalyst is to ensure the long-term operation of the hydrotreating unit.

The hydrodeasphaltene agent described in step (3) is a butterfly type, containing a carrier and molybdenum and/or tungsten loaded on the carrier, and nickel and/or cobalt, based on the total weight of the catalyst, And based on oxides, the content of molybdenum and/or tungsten is 0.5-18% by weight, the content of nickel and/or cobalt is 0.3-10% by weight, and the carrier is aluminum oxide and optional silicon oxide. The pore volume of the hydrodeasphaltene agent is not less than 0.60ml/g, preferably not less than 0.70ml/g. The asphaltene content of the feedstock designed for conventional wax oil hydrotreating units should generally be less than 500 μg/g, while the asphaltene content in FCC heavy oil is around 3000 μg/g, much higher than the design feed requirements for conventional wax oil hydrotreating units . However, asphaltene is the heaviest component in catalytic cracking heavy oil, and is the main coke precursor in catalytic cracking heavy oil. The molecular size often reaches more than ten nanometers, which easily causes coking and deactivation of conventional hydrotreating catalysts and affects Activity stability of hydrofinishing catalysts and shortening of service life of hydrofinishing catalysts. Therefore, a hydrodeasphaltene agent with a large pore volume should be filled behind the hydrogenation protecting agent, so that the asphaltenes in the catalytic cracking heavy oil can be partially removed, so as to achieve the purpose of protecting the rear hydrofinishing agent.

The hydrofinishing preparation described in step (3) is a butterfly type, containing a carrier and molybdenum and/or tungsten loaded on the carrier, and nickel and/or cobalt, based on the total weight of the catalyst, and in Based on the oxides, the content of molybdenum and/or tungsten is 10-40% by weight, the content of nickel and/or cobalt is 0.3-7% by weight, and the carrier is alumina and optionally silicon oxide. The pore volume of the hydrofinishing preparation is not less than 0.25ml/g, preferably not less than 0.30ml/g. A hydrorefining catalyst is installed behind the hydrodeasphaltene catalyst, which has high polycyclic aromatic hydrocarbon saturation activity and high desulfurization and denitrogenation activities.

The advantages of the present invention are:

1. The present invention organically combines residual oil hydrogenation, catalytic cracking heavy oil hydrogenation and catalytic cracking unit, can convert inferior residual oil into light oil products to the greatest extent, and improves the yield of gasoline and diesel oil.

2. The present invention divides catalytic cracking heavy oil into two parts, one part is used as the dilution oil of residual oil raw material, and the other part is subjected to separate hydrogenation. It not only achieves the purpose of reducing the viscosity of residual oil raw materials and promoting the reaction of residual oil hydrogenation to remove impurities, but also realizes the separate hydrofining of catalytic cracking heavy oil, avoiding heavy metals such as Ni and V in residual oil, residual carbon value and asphaltenes It can saturate most of the polycyclic aromatic hydrocarbons in the catalytic cracking heavy oil, improve its cracking performance, significantly increase the liquid yield of the catalytic cracking unit, and realize the efficient utilization of petroleum resources.

3. The present invention makes full use of the hydrogen system and high-pressure separation system of the existing residual oil hydrogenation device. Since the hydrogenation of catalytic cracking heavy oil does not require a separate hydrogen source, circulating hydrogen compressor and high-pressure separator, both investment and operating costs are low. It is much smaller than building a separate set of catalytic cracking heavy oil hydrogenation unit.

Description of drawings

Accompanying drawing is the process flow schematic diagram of the inferior residual oil processing method provided by the present invention.

Detailed ways

The method of the present invention will be further described below by means of the accompanying drawings, but the present invention is not limited thereby. As shown in the figure, the technological process of the inferior residual oil processing method provided by the present invention:

The residual oil raw material from pipeline 1 and the catalytically cracked heavy oil from pipeline 23 are mixed and then mixed with hydrogen from pipeline 9 through pipeline 2 and then enter the residual oil hydrogenation reactor 3 to react under the action of the residual oil hydrogenation catalyst. The product enters the high-pressure separator 5 through the pipeline 4, and is separated to obtain a liquid phase stream and a gas phase stream. Among them, the gas phase stream (hydrogen-rich gas) enters the compressor 7 through the pipeline 6, after boosting the pressure, mixes with the new hydrogen from the pipeline 8, and then enters the residual oil hydrogenation reactor 3 and the catalytic cracking heavy oil hydrogenation through the pipeline 9 and the pipeline 10 respectively Reactor 25. The liquid phase stream obtained by the high-pressure separator 5 enters the atmospheric tower 12 through the pipeline 11, and the gas is separated, and the hydrogenated gasoline and the hydrogenated diesel oil are respectively discharged from the device through the pipelines 13, 14 and 15, and the hydrogenated residue obtained through the separation is passed through the pipeline 16 Enter the catalytic cracking unit 17, react in the presence of a catalytic conversion catalyst, and separate the reaction products to obtain dry gas, liquefied gas, catalytic cracked gasoline and catalytic cracked diesel oil, and leave the unit through pipelines 18, 19, 20 and 21 respectively. The separated FCC heavy oil is divided into two parts, one part passes through pipelines 22 and 23 as diluent oil and mixes with the residual oil raw material from pipeline 1, and then enters the residual oil hydrogenation reactor 3, and the other part enters the FCC heavy oil through pipelines 22 and 24 for hydrogenation Reactor 25 reacts under the action of catalytic cracking heavy oil hydrogenation catalyst, and the reaction product enters high-pressure separator 5 through pipeline 26 and pipeline 4 for gas-liquid separation.

The following examples will further illustrate the present invention, but do not limit the present invention thereby.

The properties of the residue raw materials A and B adopted in Examples and Comparative Examples are shown in Table 1. The residual oil hydrogenation test was carried out in a double-tube reactor. The hydrogenation protection agent and hydrodemetallization catalyst were filled in the first reactor (referred to as the first reactor), and the hydrogenation agent was filled in the second reactor (referred to as the second reactor). Desulfurization catalyst, the ratio of the three is 5:45:50, of which the trade names of hydrogenation protection agent, hydrodemetallization catalyst, and hydrodesulfurization catalyst are RG-10A, RDM-2B, and RMS-1B, all produced by Sinopec Catalyst Branch Changling Catalyst Factory production. The catalytic conversion catalyst used in the catalytic cracking test is produced by Qilu Catalyst Factory of Sinopec Catalyst Branch Company, and the brand name is MLC-500. The ratio of hydrogenation protection agent, hydrodeasphaltenation agent and hydrofinishing agent used in the hydrogenation test of catalytic cracking heavy oil is 5:15:80, and the brand name of the hydrogenation protection agent is RG-10B, which is supplied by Sinopec Catalyst Branch Changling Catalyst Factory production. The hydrodeasphaltene agent and hydrofinishing agent were prepared in the laboratory, and their physical and chemical properties are shown in Table 2.

Example 1

The heated residual oil raw material A and FCC heavy oil are mixed with hydrogen and then enter the residual oil hydrogenation reactor to react under the action of the residual oil hydrogenation catalyst. The test conditions of the residual oil hydrogenation unit are shown in Table 3. The reactant flow enters the high-pressure separator and is separated into a gas-phase flow and a liquid-phase flow, wherein the gas-phase flow is recycled after being purified and boosted. The liquid phase stream is subjected to atmospheric pressure fractionation to obtain gas, hydrogenated gasoline, hydrogenated diesel oil and hydrogenated residue. The hydrogenated residual oil is used as the raw material of the catalytic cracking unit, and the cracking reaction is carried out in the presence of a catalytic conversion catalyst. The reaction products are separated to obtain dry gas, liquefied gas, catalytic gasoline, catalytic diesel oil and catalytic cracking heavy oil. The operating conditions of catalytic cracking are shown in Table 3. FCC heavy oil (accounting for 35% of catalytic cracking feed) is divided into two parts, one part (accounting for 14% of catalytic cracking feed) is mixed with residual oil feed as diluent oil and then enters residue hydrogenation reactor, mixed with The viscosity of residual oil raw material after catalytic cracking heavy oil is 100mm ² /s. The remaining part (accounting for 21% of the catalytic cracking feed) is mixed with hydrogen and enters the catalytic cracking heavy oil hydrogenation reactor, and reacts under the action of the catalyst, and the reactant flow enters the high-pressure separator for gas-liquid separation. The total product distribution (sum of the products of the two installations) is shown in Table 3.

Example 2

Embodiment 2 adopts residual oil raw material B. Process flow is identical with embodiment 1. Different from Example 1, the ratio of catalytic cracking heavy oil to catalytic cracking feedstock in Example 2 is 22%, wherein as the diluent oil part accounts for 6% of catalytic cracking feedstock, and the residual oil raw material after mixing catalytic cracking heavy oil The viscosity was 110 mm ² /s. The rest (accounting for 16% of the FCC feed) enters the FCC heavy oil hydrogenation reactor. The distribution of the total product of the group (the sum of the products of the two devices) is shown in Table 3.

It can be seen from Table 3 that both Example 1 and Example 2 have achieved relatively high liquid (liquefied gas+gasoline+diesel) yields, which are 81.86% and 86.43% respectively. Illustrate that adopting the method of the present invention can reduce the viscosity of raw material residual oil and promote the purpose of the removal reaction of residual oil hydrogenation impurities, and at the same time, the influence of impurities in residual oil can be avoided by the independent hydrofinishing of catalytic cracking heavy oil, and the improvement can be improved. Improve the effect of catalytic cracking heavy oil hydrogenation, improve the liquid yield of catalytic cracking unit.

Table 1

Raw oil number A B Density (20℃), kg/ ^m3 1023.8 970.0 Kinematic viscosity (100°C), ^mm2 /s 1570 281.3 Carbon residue, wt% 20.2 13.95 Nitrogen, weight % 0.33 0.26 Sulfur, wt% 5.1 3.1 Four components, weight % Saturated hydrocarbons 11.6 20.5 Aromatics 53.4 51.1 colloid 26.4 21.6 Asphaltenes (C ₇ insoluble matter) 8.6 6.8 Metal content, ppm Nickel 41 64.0 Vanadium 118 5.3

Table 2

Catalyst Hydrodeasphaltene agent   Hydrofinishing Chemical composition, wt% Nickel oxide 1.1 2.8 Molybdenum oxide 6.2 Tungsten Oxide 26.2 Physical properties: Specific surface area, m ² /g 120 170 Pore volume, ml/g 0.71 0.33  Crush strength, N/mm 11 18 shape Butterfly Butterfly

table 3

Claims (10)

1. A processing method for inferior residual oil, comprising: (1) The residual oil raw material, part of the catalytically cracked heavy oil from step (2) and hydrogen enter the residual oil hydrogenation reactor together, and react under the action of the residual oil hydrogenation catalyst, and the reactant flow enters the high-pressure separator to be separated into a gas phase Logistics and liquid phase logistics, wherein the gas phase stream is recycled after being purified and boosted, and the liquid phase stream is fractionated to obtain gas, hydrogenated gasoline, hydrogenated diesel oil and hydrogenated residue; (2), step (1) obtained hydrogenated residue enters the catalytic cracking unit, reacts in the presence of a catalytic conversion catalyst, and separates the reaction product to obtain dry gas, liquefied gas, catalytic cracked gasoline, catalytic cracked diesel oil and catalytic cracked heavy oil; (3) The catalytic cracking heavy oil obtained in step (2) is divided into two parts, one part is returned to step (1) and mixed with residual oil raw material to enter the residual oil hydrogenation reactor, and the remaining part is mixed with hydrogen to enter the catalytic cracking heavy oil hydrogenation reaction The device reacts under the effect of catalytic cracking heavy oil hydrogenation catalyst, and the reactant flow enters the high-pressure separator described in step (1) to carry out gas-liquid separation; The distillation range of the catalytic cracking heavy oil obtained in the step (2) is 260°C-550°C, based on fresh raw materials for catalytic cracking, the weight percentage of the catalytic cracking heavy oil is 12%-60%; The catalytic cracking heavy oil hydrogenation catalyst in the step (3) includes a hydrogenation protecting agent, a hydrogenation deasphaltene agent and a hydrofinishing agent in sequence according to the flow direction of the reactant stream; taking the volume of the overall catalytic cracking heavy oil hydrogenation catalyst as a benchmark, The filling volume percentages of the hydrogenation protecting agent, hydrogenation deasphaltene agent and hydrofinishing agent are respectively 2%-30%, 5%-50% and 5%-93%; The step (2) in the catalytic cracking unit: the preheated hydrogenated residual oil enters the first reaction zone of the catalytic conversion reactor under the lifting effect of water vapor to contact with the hot regenerated catalytic conversion catalyst, and the reaction temperature is 510 ° C -650°C, reaction time of 0.05 seconds to 1.0 seconds, weight ratio of catalyst to raw oil of 3-15:1, weight ratio of steam to raw oil of 0.03-0.3:1, pressure of 130kPa-450kPa A macromolecular cracking reaction occurs; the generated oil and gas and the catalytic conversion catalyst used in the first reaction zone enter the second reaction zone of the catalytic conversion reactor. Cracking reactions, hydrogen transfer reactions and isomerization reactions are carried out under these conditions. 2. according to the described method of claim 1, it is characterized in that, the reaction condition of described step (1) residual oil hydrogenation reactor is: hydrogen partial pressure 5.0MPa-22.0MPa, reaction temperature 330 ℃-450 ℃, volume The space velocity is 0.1h ^-1 -3.0h ^-1 , and the volume ratio of hydrogen to oil is 350-2000. 3. according to the described method of claim 1, it is characterized in that, described step (2) catalytic conversion catalyst comprises zeolite, inorganic oxide compound and optional clay, and each component accounts for catalyst gross weight respectively: zeolite 1 weight %- 50 wt%, inorganic oxide 5 wt%-99 wt%, clay 0 wt%-70 wt%. 4. according to the described method of claim 1, it is characterized in that, described hydrogenation protecting agent is Raschig cyclic, contains a kind of alumina carrier and molybdenum and/or tungsten loaded on the alumina carrier, and Nickel and/or cobalt, based on the total weight of the hydrogenation protection agent, and calculated as oxides, the content of molybdenum and/or tungsten is 1-10% by weight, and the content of nickel and/or cobalt is 0.5-3% by weight ; the alumina is γ-alumina; the pore volume of the hydrogenation protecting agent is not less than 0.50ml/g. 5. according to the described method of claim 1, it is characterized in that, described hydrodeasphaltene agent is butterfly type, contains a kind of carrier and molybdenum and/or tungsten loaded on the carrier, and nickel and/or Cobalt, based on the total weight of the hydrodeasphaltene agent, and as an oxide, the content of molybdenum and/or tungsten is 0.5-18% by weight, the content of nickel and/or cobalt is 0.3-10% by weight, the carrier It is aluminum oxide and optional silicon oxide; the pore volume of the hydrodeasphaltene agent is not less than 0.60ml/g. 6. according to the described method of claim 1, it is characterized in that, described hydrofinishing preparation is butterfly type, contains a kind of carrier and molybdenum and/or tungsten loaded on the carrier, and nickel and/or cobalt, Based on the total weight of the hydrofinishing preparation and calculated as oxides, the content of molybdenum and/or tungsten is 10-40% by weight, the content of nickel and/or cobalt is 0.3-7% by weight, and the carrier is alumina and Optional silicon oxide; the pore volume of the hydrofinishing agent is not less than 0.25ml/g. 7. The method according to claim 1, characterized in that, said step (3) reaction conditions of catalytic cracking heavy oil hydrogenation reactor: reaction temperature 330°C-410°C, hydrogen partial pressure 5.0MPa-22.0MPa, volume empty The speed is 0.3h ^-1 -2.0h ^-1 , and the volume ratio of hydrogen to oil is 350-2000. 8. The method according to claim 1, characterized in that the residual oil raw material is atmospheric residual oil and/or vacuum residual oil, the viscosity is 500mm ² /s-3000mm ² /s, and the viscosity refers to 100 °C kinematic viscosity. 9. according to the described method of claim 1, it is characterized in that, in step (1), take residual oil raw material as a benchmark, catalytic cracking heavy oil is used as the dilution oil of residual oil raw material, and blending ratio is 5 weight %-20 weight % %, the viscosity of the residual oil raw material after being mixed with catalytic cracking heavy oil is 50mm ² /s-300mm ² /s, and the viscosity mentioned refers to the kinematic viscosity at 100°C. 10. The method according to claim 9, characterized in that the viscosity of the residual oil raw material after adding catalytic cracking heavy oil is 100mm ² /s-200mm ² /s, and the viscosity refers to the kinematic viscosity at 100°C .

Images