CN117603730A - Cooling separation method for tail oil circulation type heavy oil suspension bed hydrocracking product thermal high-pressure oil - Google Patents

Abstract

According to the cooling separation method of the tail oil circulation type heavy oil suspension bed hydrocracking product thermal high-fraction oil, aromatic hydrocarbon-rich and easily-evaporated quenching oil KGS forms a base stream MCP-CS after being mixed and absorbed by a cooling stabilizing part DT10 of a hydrocarbon stream based on the thermal high-fraction oil, and most of the quenching oil KGS is gasified in a separation/fractionation part S50 of the base stream MCP-CS and enters flash evaporation steam of the base stream MCP-CS, so that heat absorbed by the cooling stabilizing part DT10 is brought into the flash evaporation steam of the base stream MCP-CS to be utilized, and in the condensation process of the flash evaporation steam of the base stream MCP-CS, most of vapor phase components from the quenching oil KGS finish the condensation process to release heat and can be converted into the quenching oil KGS for recycling; the method has the advantages of generating vaporization heat at low cost, realizing clean heat transfer, enhancing fractionation function and realizing similar material flow combined fractionation at low cost, and is a heat-carrying fractionation path different from a heat low-fraction oil heat-carrying to reduced pressure distillation process.

Description

Cooling and separation of thermal high-fractionated oil produced by tail oil circulation type heavy oil suspension bed hydrocracking method

Technical field

The present invention relates to a cooling and stabilizing process and a separation/fractionation process of tail oil circulation type heavy oil suspended bed hydrocracking product thermal high-fractionation oil, and in particular to a method of transferring the heat released in the cooling and stabilizing process to be used as vaporization heat or evaporation heat in the distillation process. .

Background technique

The basic idea of the present invention is: a cooling and separation method for tail oil circulation type heavy oil suspension bed hydrocracking product hot high-fractionated oil, aromatics-rich and easily evaporated quench oil KGS in the cooling stable part DT10 of the hydrocarbon stream based on hot high-fractionated oil After mixing and absorbing heat, the basic stream MCP-CS is formed, and most of the quenching oil KGS is vaporized in the separation/fractionation part S50 of the basic stream MCP-CS and enters the flash gas of the basic stream MCP-CS, thus will be in the cooling and stabilizing part The heat absorbed by DT10 is brought into the flash gas of the basic logistics MCP-CS and utilized. During the condensation process of the flash gas of the basic logistics MCP-CS, most of the vapor phase components from the quench oil KGS complete the condensation process and release heat. , and can be converted into quenching oil KGS for recycling; the advantage is that it generates vaporization heat at low cost, realizes clean heat transfer at low cost, enhances the fractionation function, and realizes joint fractionation of similar logistics. It is a different path from thermal low-fraction oil to vacuum distillation. The heat-carrying fractionation path of the process.

In order to utilize the heat energy transferred from the thermal high-fractionated oil in the cooling thermal stabilization process for the hydrocarbon fractionation process, the patent application 202211666910.4 heavy oil suspension bed hydrogenation conversion method on December 21, 2022 proposed to directly use wax oil or even The method of using a mixed oil containing a vacuum residue component of the diesel component as the quenching oil, using the vacuum residue component in the quenching oil as a heat carrier component, to treat the wax oil or even diesel components in the quenching oil. The evaporation process transports heat energy. Of course, the heat absorbed by the wax oil and even diesel components in the quenching oil during the cooling and thermal stabilization process of the hot high-fractionated oil is also part of the heat source of the evaporation process; at the same time, patent application 202211666910.4 also proposes cyclic vacuum distillation The process base oil is used as the quenching oil. The vacuum residual oil component in the quenching oil is used as the heat carrier component. The heat absorbed during the cooling and thermal stabilization process of the hot high-fractionated oil can be used as the evaporation heat of the materials in the vacuum distillation process. source, thereby reducing the evaporation temperature in the decompression process, which also implies that the bottom oil in the circulating vacuum distillation process serves as a quenching oil and helps to jointly fractionate certain mixed hydrocarbon liquids; this method involves a cooling and stabilizing method and a fractionation method for hot high-fractionated oil , but does not involve the technical solution of the present invention.

In order to use the heat energy contained in the cooled and thermally stabilized hot high-fractionated oil to separate part or all of the cold high-fractionated oil, patent application 202310828045.7 is a method for separating diesel from cold high-fractionated oil produced by heavy oil suspension bed hydrocracking. The separation process of the cold high-fractionation oil is combined with the vacuum fractionation process of the hot high-fractionation oil after cooling and thermal stabilization, which plays the role of the cold high-fractionation oil as a heat trap for medium-temperature heat and doubles as the decompression fractionation of the hot high-fractionation oil. The internal reflux liquid in the process eliminates the cold reflux load in the middle stage of the vacuum fractionation process of a portion of hot high-fraction oil; in the above operation process, a sufficient amount of hydrocarbon oil vapor is the basis for providing the heat source for component fractionation; this method does not involve Solution of the present invention.

When the present invention introduces the above-mentioned comparative documents, the heavy oil properties, tail oil properties, catalyst properties, hydrogenation targets, operating conditions, and product properties involved in the comparative documents become part of the background information of the present invention.

The method of the present invention can be selected and used according to needs, and can be used for newly built devices or renovation tasks of existing devices.

The method of the present invention has not been reported.

Therefore, the first object of the present invention is to propose a method for cooling and separating the thermal high-fractionated oil produced by tail oil circulation type heavy oil suspension bed hydrocracking.

The second purpose of the present invention is to propose a low-cost way to utilize the heat of the cooling and stabilizing process of hot high-fractionated oil to increase the fractionation function and fractionation accuracy of the separation and/or distillation process S01 of hot low-fractionated gas to obtain a thermal state. Diesel fractions and can co-fractionate thermal high-fractionated oil-based streams.

The third object of the present invention is to propose a heat transfer path in the rectification section S02 that is different from the thermal low-fraction oil to the decompression flash steam of the thermal low-fraction oil-based stream, and to increase the separation and/or separation of the rectification section S02. Or the fractionation function and fractionation accuracy of the distillation process can be used to obtain hot diesel fractions and wax oil fractions, and can jointly fractionate streams based on hot high-fractionated oil.

The fourth object of the present invention is to propose a heat transfer path in the distillation section S02 of the vacuum flash steam that is different from the thermal low-fractionated oil carrying heat to the thermal low-fractionated oil-based stream. The circulating quenching oil of the rectification section S02 of the vacuum flash steam increases the separation function and fractionation accuracy of the rectification section S02 and/or the distillation process to obtain hot diesel fractions and wax oil fractions, and can be combined with fractionation based on Logistics of hot high fraction oil.

Contents of the invention

The tail oil circulation type heavy oil suspension bed hydrocracking product thermal high-fractionation oil cooling and separation method of the present invention is characterized by:

The heavy oil suspended bed hydroconversion process U100 for converting heavy oil into low molecular weight hydrocarbons includes a reaction part R10 for carrying out heavy oil suspended bed hydroconversion, a hydrocarbon component with a conventional boiling point lower than 530°C based on the reaction product R10P and a conventional boiling point higher than 530℃ hydrocarbon component asphaltene-containing stream MCP injection quench oil KGS cooling stabilization part DT10, basic stream MCP-CS separation/fractionation part S50, vacuum flash bottom oil discharge part, vacuum flash bottom Oil circulation part and quenching oil supply part K100;

In the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in heavy oil R10F is greater than 30%;

⑴ In the reaction part R10 of heavy oil suspended bed hydrogenation conversion, in the presence of hydrogen, conventional liquid hydrocarbons, and the solid particle catalyst R10-CAT for heavy oil suspended bed hydrogenation conversion, there is or is not the presence of hydrogen-donating hydrocarbons, and the presence or absence of other solid particles. Under the condition of miscible materials, heavy oil R10F and circulating vacuum flash oil S50-FL-TOR10 from the vacuum flash bottom oil circulation part are converted into heavy oil suspension bed hydrogenation conversion reaction R10R including suspension bed hydrocracking reaction. Product R10P;

The solid particle catalyst R10-CAT contains at least Mo element, and the main working form of Mo in the reaction part R10 is M0S2;

Heavy oil R10F, whose conventional boiling point is higher than 530°C and the weight concentration of hydrocarbon components is greater than 50%, contains one or more impurity components such as asphaltenes, organic sulfur, organic nitrogen, and organic metals;

Heavy oil R10F is used as the fresh reaction feed of the reaction part R10, which is a mixed raw material of a single property of raw oil or several different properties of branch raw materials;

When heavy oil R10F is mixed from several split feed oils with different properties, at least one split feed oil contains asphaltenes, and one or several other split feed oils may or may not contain asphaltenes;

The heavy oil suspended bed hydroconversion reaction R10R includes a suspended bed hydrocracking reaction, which allows at least a part of the hydrocarbon components in the heavy oil R10F with a conventional boiling point higher than 530°C to complete the hydrocracking reaction and convert it into hydrocarbon products with smaller molecular weights;

The heavy oil suspended bed hydroconversion reaction R10R includes a suspended bed hydrofinishing reaction, which enables at least a part of the impurity elements in the heavy oil R10F to complete a hydrogenation and deimpurity reaction, and makes at least a part of the unsaturated carbon-carbon bonds of at least a part of the hydrocarbon components in the heavy oil R10F Be saturated with hydrogenation; the hydrogenation and impurity removal reaction includes one or more of a hydrodemetallization reaction, a hydrodesulfurization reaction, a hydrodenitrification reaction, and a hydrodeoxygenation reaction;

The average asphaltene weight concentration of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average asphaltene weight concentration of the heavy oil R10F;

The average Conian carbon residue value of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average Conian carbon residue value of heavy oil R10F;

The average organic sulfur weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average organic sulfur weight content of heavy oil R10F;

The average organic nitrogen weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average organic nitrogen weight content of heavy oil R10F;

The average organic metal weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average organic metal weight content of heavy oil R10F;

In the hot high-pressure separation part S10, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C based on the reaction product R10P is separated into hot high-fractionated gas S10-V and hot high-fractionated oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

An asphaltene-containing stream based on the quenched mixture stream MCP-BASE containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the base stream MCP-CS;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash distillation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in the external discharge vacuum flash evaporation bottom oil S50-FL-OUT is lower than 70% of the weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in heavy oil R10F. %;

⑸ In the vacuum flash evaporation bottom oil circulation part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash evaporation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is returned to the reaction part R10 as circulating vacuum flash oil S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating vacuum flash oil S50-FL-TOR10 or the circulating vacuum flash oil S50-FL-TOR10 is mixed and contacted with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F;

⑹ In the quenching oil supply part K100, the quenching oil KGS is a hydrocarbon oil rich in aromatics, and most of the quenching oil KGS vaporizes in the separation/fractionation part S50 and enters the flash gas of the basic stream MCP-CS, which will be cooled during the cooling process. The heat absorbed by the stabilizing part DT10 is brought into the flash gas of the basic stream MCP-CS and utilized. During the condensation process of the flash gas of the basic stream MCP-CS, most of the vapor phase components from the quench oil KGS complete the condensation process. Release heat.

In the present invention, generally, in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in the heavy oil R10F is greater than 50%;

⑴ In the reaction part R10 of the heavy oil suspended bed hydrogenation conversion, the heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 70%, and at least one of the following conditions is met:

① Asphaltene weight concentration is greater than 12%;

②Kang’s carbon residue value is higher than 16%;

③The weight content of organic sulfur is higher than 0.5%;

④The weight content of organic nitrogen is higher than 0.15%;

⑤The organic metal weight content is higher than 0.015%;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

In the cooling stabilization part DT10, the logistics MCP with a temperature of T1 is mixed with the quenching oil KGS with a temperature of T3 to become a quenched mixed flow MCP-BASE with a temperature of T2. The cooling range of the logistics MCP is DT, DT=T1-T2, DT 15～80℃;

Logistics MCP is selected from one or more of the following logistics:

①The reaction product R10P is used as logistics MCP;

②Thermal high-percentage oil S10-L is used as logistics MCP;

③The vapor-liquid miscible material formed by hot high-percentage oil S10-L after decompression is used as logistics MCP;

④The vapor-liquid miscible material formed by the hot high-fragment oil S10-L after decompression is separated into first-level hot low-pressure flash steam and first-level hot low-pressure flash oil in the first-level hot low-pressure flash evaporation process; the first-level hot low-pressure flash evaporation process The operating pressure is greater than atmospheric pressure;

First-grade hot low-pressure flash oil, used as logistics MCP;

⑤The vapor-liquid miscible material formed by the hot high-fraction oil S10-L after decompression is separated into first-level hot low-pressure flash steam and first-level hot low-pressure flash oil in the first-level hot low-pressure flash evaporation process; the first-level hot low-pressure flash evaporation process The operating pressure is greater than atmospheric pressure;

After the pressure of the primary hot low-pressure flash oil is reduced, it is separated into secondary hot low-pressure flash steam and secondary hot low-pressure flash oil in the second-stage hot low-pressure flash evaporation process; the operating pressure of the second-stage hot low-pressure flash evaporation process is greater than atmospheric pressure;

Secondary hot low-pressure flash oil, used as logistics MCP;

⑥The vapor-liquid miscible material formed by the hot high-fractionated oil S10-L after decompression is separated into hot low-pressure flash steam and hot low-pressure flash oil during the hot low-pressure flash evaporation process. The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

After decompression, the hot low-pressure flash oil enters the flash evaporation process of negative pressure operation. After the depressurization, the hot low-pressure flash oil enters the negative pressure operation state and the operating pressure is greater than the atmospheric pressure. It is used as logistics MCP.

In the present invention, generally, in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in the heavy oil R10F is greater than 50%;

⑴ In the reaction part R10 of heavy oil suspended bed hydrogenation conversion, in the presence of hydrogen, conventional liquid hydrocarbons, and the solid particle catalyst R10-CAT for heavy oil suspended bed hydrogenation conversion, there is or is not the presence of hydrogen-donating hydrocarbons, and the presence or absence of other solid particles. Under the condition of mixed phase materials, heavy oil R10F undergoes heavy oil suspended bed hydrogenation conversion reaction R10R including suspended bed hydrocracking reaction and is converted into reaction product R10P;

The solid particle catalyst R10-CAT contains at least Mo element, and the main working form of Mo in the reaction part R10 is M0S2;

Heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 70%, and meets at least one of the following conditions:

① Asphaltene weight concentration is greater than 12%;

②Kang’s carbon residue value is higher than 16%;

③The weight content of organic sulfur is higher than 0.5%;

④The weight content of organic nitrogen is higher than 0.15%;

⑤The organic metal weight content is higher than 0.015%;

In the reaction part R10, the single-pass weight conversion rate of hydrocracking of hydrocarbon components with conventional boiling points higher than 530°C in all feed oils is greater than 20%, so that at least 50% by weight of asphaltenes in the heavy oil R10F complete the hydrocracking reaction; All feed oils in the reaction section R10, including heavy oil R10F and circulating vacuum flash oil S50-FL-TOR10 from the vacuum flash bottom oil circulation section;

The heavy oil suspended bed hydroconversion reaction R10R includes a suspended bed hydrofinishing reaction, which enables at least 80% by weight of the organic metals in the heavy oil R10F to complete the hydrodemetallization reaction and completes the hydrogenation of at least 60% by weight of the organic sulfur in the heavy oil R10F. The desulfurization reaction is to complete the hydrodenitrification reaction of at least 30% by weight of organic nitrogen in the heavy oil R10F, so that the average Conian carbon residue value of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average Conian carbon residue value of the heavy oil R10F. 50%;

In the hot high-pressure separation part S10, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C based on the reaction product R10P is separated into hot high-fractionated gas S10-V and hot high-fractionated oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

An asphaltene-containing stream based on the quenched mixture stream MCP-BASE containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the base stream MCP-CS;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash distillation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in the external discharge vacuum flash evaporation base oil S50-FL-OUT is lower than 50% of the weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in heavy oil R10F. %;

⑸ In the vacuum flash evaporation bottom oil circulation part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash evaporation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is returned to the reaction part R10 as circulating vacuum flash oil S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating vacuum flash oil S50-FL-TOR10 or the circulating vacuum flash oil S50-FL-TOR10 is mixed and contacted with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F;

⑹ In the quenching oil supply part K100, the quenching oil KGS is selected from one or more of the following oils:

① In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280℃, and the temperature of the quenching oil KGS is higher than the temperature of the initial quenching oil KGS0 At least 40℃;

②In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270℃, and the temperature of the quenching oil KGS is higher than that of the initial quenching oil KGS0. The temperature is at least 40℃;

③ A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, the operating conditions are usually as follows: in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in the heavy oil R10F is 75 to 98%;

⑴In the reaction part R10, the weight content of MOS2 in the liquid phase of the reaction process is 0.1~0.5%;

Heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 85%, and meets at least one of the following conditions:

① Asphaltene weight concentration is greater than 16%;

②Kang’s carbon residue value is higher than 24%;

③The weight content of organic sulfur is higher than 2.5%;

④The weight content of organic nitrogen is higher than 0.25%;

⑤The organic metal weight content is higher than 0.025%;

The operating conditions of reaction part R10 are: temperature 380~460℃, pressure 8.0~25.0MPa, hydrogen/raw oil volume ratio 50~4000, volume space velocity 0.1~10.0hr ^-1 ; weight chemical hydrogen of heavy oil R10F Consumption is 0.05~4.00%;

The operating conditions of the hot high-pressure separation part S10 are: the temperature is 360~460°C, the pressure is 8.0~25.0MPa, and hydrogen is injected or not injected into the liquid phase zone of the hot high-fraction oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

In the cooling stabilization part DT10, the logistics MCP with a temperature of T1 is mixed with the quenching oil KGS with a temperature of T3 to become a quenched mixed flow MCP-BASE with a temperature of T2. The cooling range of the logistics MCP is DT, DT=T1-T2, DT 25～75℃;

The ratio of the weight flow rate of quench oil KGS to the weight flow rate of logistics MCP is 0.01 to 0.65;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

The gas MCP-CS-FV composed of low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash distillation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The ratio of the weight flow rate of the hydrocarbon components with a conventional boiling point higher than 530°C in the vented vacuum flash bottom oil S50-FL-OUT to the weight flow rate of the hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F , less than 25%;

⑸ In the vacuum flash evaporation base oil circulation part, the ratio of the weight flow rate of the circulating vacuum flash oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 0.5 to 2.0.

In the present invention, the operating conditions are generally as follows: in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F is 88 to 95%;

⑴In the reaction part R10, the weight content of MOS ₂ in the liquid phase of the reaction process is 0.2 to 0.4%;

Heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 90%, and meets at least one of the following conditions:

① Asphaltene weight concentration is greater than 20%;

②Kang’s carbon residue value is higher than 28%;

③The weight content of organic sulfur is higher than 3.5%;

④The weight content of organic nitrogen is higher than 0.45%;

⑤The organic metal weight content is higher than 0.050%;

The operating conditions of reaction part R10 are: temperature 400~440℃, pressure 10.0~17.0MPa, hydrogen/raw oil volume ratio 100~1500, volume space velocity 0.2~2.0hr ^-1 ; weight chemical hydrogen of heavy oil R10F Consumption is 2.00~3.50%;

The operating conditions of the hot high-pressure separation part S10 are: the temperature is 360~440℃, the pressure is 10.0~17.0MPa, and hydrogen is injected or not injected into the liquid phase zone of the hot high fraction oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quench oil KGS to become a post-quench mixture. LogisticsMCP-BASE;

In the cooling stabilization part DT10, the logistics MCP with a temperature of T1 is mixed with the quenching oil KGS with a temperature of T3 to become a quenched mixed flow MCP-BASE with a temperature of T2. The cooling range of the logistics MCP is DT, DT=T1-T2, DT is 35~65℃;

The ratio of the weight flow rate of quench oil KGS to the weight flow rate of logistics MCP is 0.01 to 0.65;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

The gas MCP-CS-FV composed of low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT based on the vacuum flash distillation bottom oil S50-FL is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The ratio of the weight flow rate of the hydrocarbon components with a conventional boiling point higher than 530°C in the vented vacuum flash bottom oil S50-FL-OUT to the weight flow rate of the hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F , less than 12%;

⑸ In the vacuum flash evaporation base oil circulation part, the ratio of the weight flow rate of the circulating vacuum flash oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 1.0 to 2.0.

In the present invention, heavy oil R10F can be selected from one or more of the following streams:

①The bottom oil in the vacuum distillation process of crude oil;

②The base oil in the vacuum distillation process of shale oil;

③The base oil in the vacuum distillation process of oil sand oil;

④The base oil in the coal tar vacuum distillation process;

⑤Solvent deasphalted oil.

In the present invention, the quenching oil KGS can be one or more of the following oils:

① The condensate oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50;

② A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, usually, (3) in the separation/fractionation part S50, the hot high-fractionated oil S10-L is depressurized to obtain the miscible material S10-L-DP;

The miscible material S10-L-DP enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating conditions of the first hot low-pressure flash evaporation process are: the temperature is 340~440°C, The pressure is 0.35~2.0MPa; the first hot low fraction oil may or may not be in contact with the stripping water vapor;

After the pressure of the first hot low-separation oil is reduced, it enters the second hot low-pressure flash evaporation process and is separated into the second hot low-separation gas and the second hot low-separation oil; the operating conditions of the second hot low-pressure flash evaporation process are: the temperature is 330 ~ 430 ℃, pressure is 0.15~0.30MPa; the second thermal low-fractionated oil may or may not be in contact with the stripping water vapor; the operating pressure of the second thermal low-pressure flash evaporation process is lower than the operating pressure of the first thermal low-pressure flash evaporation process;

The second hot low-fractionated oil is depressurized and enters the first negative pressure flash evaporation process to be separated into the first negative pressure flash steam and the first negative pressure flash evaporation oil; the operating conditions of the first negative pressure flash evaporation process are: the temperature is 325 ~ 415℃, pressure is -0.55~-0.098MPa; the first negative pressure flash oil is in contact with or not in contact with the stripping water vapor; the operating pressure of the first negative pressure flash evaporation process is lower than that of the second hot low pressure flash evaporation process operating pressure;

The first negative pressure flash oil is used as the base oil of vacuum flash evaporation S50-FL;

The first hot low-component gas enters or does not enter the first hot low-component gas for separation in the distillation process;

The second hot low-component gas enters or does not enter the second hot low-component gas for separation in the distillation process;

The first thermal low-gas distillation process and the second thermal low-gas distillation process are set up separately or share a set of distillation processes;

The first negative pressure flash steam enters or does not enter the first negative pressure flash steam rectification process for separation;

The flash steam from the first hot low-pressure flash evaporation process is directly discharged from the first hot low-pressure flash evaporation process, or mixed with the liquid from the first hot low-pressure vapor distillation process and then discharged from the first hot low-pressure flash evaporation process.

The flash steam from the second hot low-pressure flash evaporation process is directly discharged from the second hot low-pressure flash evaporation process, or mixed with the liquid from the second hot low-pressure vapor distillation process and then discharged from the second hot low-pressure flash evaporation process.

The flash steam from the first negative pressure flash evaporation process is directly discharged from the first negative pressure flash evaporation process, or mixed with the liquid from the first negative pressure flash steam distillation process and then discharged from the first negative pressure flash evaporation process.

In the present invention, generally, (3) in the separation/fractionation part S50, the miscible material S10-L-DP is obtained after depressurizing the hot high-fractionated oil S10-L;

The miscible material S10-L-DP enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating conditions of the first hot low-pressure flash evaporation process are: the temperature is 340~440°C, The pressure is 0.35~2.0MPa; the first hot low fraction oil may or may not be in contact with the stripping water vapor;

After the pressure of the first hot low-separation oil is reduced, it enters the second hot low-pressure flash evaporation process and is separated into the second hot low-separation gas and the second hot low-separation oil; the operating conditions of the second hot low-pressure flash evaporation process are: the temperature is 330 ~ 430 ℃, pressure is 0.15~0.30MPa; the second thermal low-fractionated oil may or may not be in contact with the stripping water vapor; the operating pressure of the second thermal low-pressure flash evaporation process is lower than the operating pressure of the first thermal low-pressure flash evaporation process;

The second hot low-fractionated oil is depressurized and enters the first negative pressure flash evaporation process to be separated into the first negative pressure flash steam and the first negative pressure flash evaporation oil; the operating conditions of the first negative pressure flash evaporation process are: the temperature is 325 ~ 415℃, pressure is -0.55~-0.098MPa; the first negative pressure flash oil is in contact with or not in contact with the stripping water vapor; the operating pressure of the first negative pressure flash evaporation process is lower than that of the second hot low pressure flash evaporation process operating pressure;

After the first negative pressure flash oil is decompressed, it enters the second negative pressure flash evaporation process and is separated into the second negative pressure flash steam and the second negative pressure flash oil; the operating conditions of the second negative pressure flash evaporation process are: the temperature is 345 ~405℃, pressure is -0.090~-0.098MPa; in the second heat, the low fraction oil is in contact with or not in contact with the stripping water vapor; the operating pressure of the second negative pressure flash evaporation process is lower than that of the first negative pressure flash evaporation process operating pressure;

The second negative pressure flash oil is used as vacuum flash evaporation base oil S50-FL;

The first hot low-component gas enters or does not enter the first hot low-component gas for separation in the distillation process;

The second hot low-component gas enters or does not enter the second hot low-component gas for separation in the distillation process;

The first thermal low-gas distillation process and the second thermal low-gas distillation process are set up separately or share a set of distillation processes;

The first negative pressure flash steam enters or does not enter the first negative pressure flash steam rectification process for separation;

The second negative pressure flash steam enters or does not enter the second negative pressure flash steam rectification process for separation;

The first negative pressure flash steam distillation process and the second negative pressure flash steam distillation process are set separately or share a set of distillation processes;

The flash steam from the first hot low-pressure flash evaporation process is directly discharged from the first hot low-pressure flash evaporation process, or mixed with the liquid from the first hot low-pressure vapor distillation process and then discharged from the first hot low-pressure flash evaporation process.

The flash steam from the second hot low-pressure flash evaporation process is directly discharged from the second hot low-pressure flash evaporation process, or mixed with the liquid from the second hot low-pressure vapor distillation process and then discharged from the second hot low-pressure flash evaporation process.

The flash steam from the first negative pressure flash evaporation process is directly discharged from the first negative pressure flash evaporation process, or mixed with the liquid from the first negative pressure flash steam distillation process and then discharged from the first negative pressure flash evaporation process;

The flash steam from the second negative pressure flash evaporation process is directly discharged from the second negative pressure flash evaporation process, or mixed with the liquid from the second negative pressure flash steam distillation process and then discharged from the second negative pressure flash evaporation process.

In the present invention, generally, the distillation bottom oil discharged from the flash steam rectification process of the first hot low-pressure flash evaporation process and/or the distillation bottom oil discharged from the flash steam rectification process of the second hot low-pressure flash evaporation process enters The first hot low-pressure flash evaporation process and/or the second hot low-pressure flash evaporation process are in mixed contact with the flash steam of the first hot low-pressure flash evaporation process and/or the flash steam of the second hot low-pressure flash evaporation process, as a wash oil washing flash. Heavy components and solid particles in steam.

In the present invention, generally, the distillation bottom oil discharged from the flash steam distillation process of the first negative pressure flash evaporation process and/or the distillation bottom oil discharged from the flash steam distillation process of the second negative pressure flash evaporation process enters The first negative pressure flash evaporation process and/or the second negative pressure flash evaporation process are in mixed contact with the flash steam of the first negative pressure flash evaporation process and/or the flash steam of the second negative pressure flash evaporation process, as a washing oil washing flash. Heavy components and solid particles in steam.

In the present invention, generally, the waxy oil component liquid stream discharged from the negative pressure distillation process of flash steam in the negative pressure flash evaporation process enters the first hot low pressure flash evaporation process and/or the second hot low pressure flash evaporation process, and is combined with the third hot low pressure flash evaporation process. The flash steam of the first hot low-pressure flash evaporation process and/or the flash steam of the second hot low-pressure flash evaporation process are mixed and contacted to wash the heavy components and solid particles in the flash steam of the washing oil.

In the present invention, generally, the waxy oil-containing liquid that does not contain vacuum residue is obtained by the distillation process of the flash steam of the first hot low-pressure flash evaporation process and/or the flash steam distillation process of the second hot low-pressure flash evaporation process. The phase hydrocarbon oil stream enters the negative pressure distillation process of the flash steam of the negative pressure flash evaporation process and is used as an intermediate feed.

In the present invention, usually, (3) in the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recovered;

In the separation recovery system S50-VD, based on the heat released by the condensation process of the gas MCP-CS-FV, the initial quench oil KGS0 from the quench oil supply part K100 is heated in the indirect heating step HX6030 to obtain the preheated initial quench oil KGS0- H, the flow based on the initial quenching oil KGS0-H after preheating is used as quenching oil KGS to enter the cooling stabilization part DT10;

The component composition of the quenching oil KGS is the same as or different from the component composition of the initial quenching oil KGS0. The weight flow rate of the quenching oil KGS is the same as or different from the weight flow rate of the initial quenching oil KGS0; the initial quenching oil KGS0 preheating changes to preheating The process of post-initial quenching oil KGS0-H, including or not including flash evaporation process, including or not including fractionation process;

⑹In the quenching oil supply part K100, provide initial quenching oil KGS0;

The initial quench oil KGS0 is the condensed oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50. It is preheated by the indirect heating step HX6030 in the separation/fractionation section S50 to obtain the quench oil KGS;

The initial quenching oil KGS0 is one or more of the following oils:

① In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280℃, and the temperature of the quenching oil KGS is higher than the temperature of the initial quenching oil KGS0 At least 40℃;

②In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270℃, and the temperature of the quenching oil KGS is higher than that of the initial quenching oil KGS0. The temperature is at least 40℃;

③ A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, usually, (3) in the separation/fractionation part S50, during normal operation, there is no oil heating furnace to provide heat, that is, no oil heating furnace is installed or the heating furnace through which the oil passes does not provide heat.

In the present invention, generally, (5) in the vacuum flash evaporation bottom oil circulation part, the ratio of the weight flow rate of the circulating vacuum flash evaporation oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 1.0 to 2.0.

The present invention, generally, (2) in the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the thermal high-fractionated oil S10-L containing hydrocarbon components with a conventional boiling point higher than 530°C, and the quenching oil KGS based on the separation/fractionation part S50 After mixing, it becomes basic logistics MCP-CS;

⑶In the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

In the separation recovery system S50-VD, based on the heat released during the condensation process of the gas MCP-CS-FV, the initial quenching oil KGS0 is heated in the indirect heating step HX6030 to obtain the preheated initial quenching oil KGS0-H. Based on the initial quenching oil KGS0-H after preheating, The flow of quenching oil KGS0-H is used as quenching oil KGS to enter the cooling stabilization part DT10;

The component composition of the quenching oil KGS is the same as or different from the component composition of the initial quenching oil KGS0. The weight flow rate of the quenching oil KGS is the same as or different from the weight flow rate of the initial quenching oil KGS0; the initial quenching oil KGS0 preheating changes to preheating The process of post-initial quenching oil KGS0-H, including or not including the flash evaporation process KGSO-FPR, including or not including the fractionation process KGSO-DPR;

The flash steam of the flash evaporation process KGSO-FPR and/or the gas products of the fractionation process KGSO-DPR enter or do not enter the separation and recovery system S50-VD of the gas MCP-CS-FV;

⑹In the quenching oil supply part K100, provide initial quenching oil KGS0;

The initial quenching oil KGS0 is preheated by the indirect heating step HX6030 in the separation/fractionation section S50 to obtain the quenching oil KGS;

The initial quenching oil KGS0 is one or more of the following oils:

① In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280℃, and the temperature of the quenching oil KGS is higher than the temperature of the initial quenching oil KGS0 At least 40℃;

②In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270℃, and the temperature of the quenching oil KGS is higher than that of the initial quenching oil KGS0. The temperature is at least 40℃;

③ A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, usually, (3) in the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recovered;

In the separation recovery system S50-VD, based on the heat released during the condensation process of the gas MCP-CS-FV, the initial quenching oil KGS0 is heated in the indirect heating step HX6030 to obtain the preheated initial quenching oil KGS0-H. Based on the initial quenching oil KGS0-H after preheating, The flow of quenching oil KGS0-H is used as quenching oil KGS to enter the cooling stabilization part DT10;

After the initial quenching oil KGS0 is converted into the preheated initial quenching oil KGS0-H, the indirect heating step HX6030 uses at least 2 series preheating processes. The initial quenching oil KGS0 undergoes an upstream preheating process and then performs a flash operation to obtain the removal steam. The liquid enters the adjacent downstream preheating process, and finally the preheated initial quench oil KGS0-H discharged from the indirect heating step HX6030 is flash evaporated to remove the vapor KGS0-H-V and the liquid is used as quench oil KGS.

In the present invention, generally, in the indirect heating step HX6030, the gas KGSO-H-V enters the fractionation tower of the separation and recovery system S50-VD of the gas MCP-CS-FV.

In the present invention, usually, (3) in the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280°C, and the temperature of the quenching oil KGS is higher than the initial The temperature of the quenching oil KGS0 is at least 40°C.

In the present invention, usually, (3) in the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270°C, and the temperature of the quenching oil KGS is higher than The initial temperature of the quench oil KGS0 is at least 40°C.

In the present invention, (1) hydrogen-donating hydrocarbons can be used in the reaction part R10 of the heavy oil suspended bed hydrogenation conversion.

In the present invention, generally, (2) in the cooling stabilization section DT10, the asphaltene-containing stream MCP based on the thermal high-fractionation oil S10-L containing hydrocarbon components with a conventional boiling point higher than 530°C is combined with the quenching oil KGS from the separation/fractionation section S50 After mixing, it becomes basic logistics MCP-CS;

⑶In the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

In the separation recovery system S50-VD, based on the heat released during the condensation process of the gas MCP-CS-FV, the initial quenching oil KGS0 is heated in the indirect heating step HX6030 to obtain the preheated initial quenching oil KGS0-H. Based on the initial quenching oil KGS0-H after preheating, The flow of quenching oil KGS0-H is used as quenching oil KGS to enter the cooling stabilization part DT10;

⑹ In the quench oil supply section K100, the initial quench oil KGS0 is the condensed oil BASE-KGS0 obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50. The distillate oil BASE-KGS0 is first boosted and then heated. The materials are used as quenching oil KGS.

In the present invention, usually, in the (3) separation/fractionation part S50, the temperature of the initial quenching oil KGS0 is 110~200°C, and the temperature of the quenching oil KGS is 230~300°C.

In the present invention, generally, in the (3) separation/fractionation part S50, the temperature of the initial quenching oil KGS0 is 130~180°C, and the temperature of the quenching oil KGS is 260~290°C.

In the present invention, usually (2) in the cooling stable part DT10, the ratio of the weight flow rate of the quenching oil KGS to the weight flow rate of the logistics MCP is 0.01 to 0.15 or 0.15 to 0.30 or 0.30 to 0.45 or 0.45 or more.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is circulating oil;

Quench oil KGS is the condensed oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50;

Basic logistics MCP-CS is selected from one or more of the following logistics:

① The mixed-phase stream formed by depressurizing the hot high-fragment oil S10-L is used as the logistics MCP, and is mixed with the quenching oil KGS to become the basic logistics MCP-CS;

② The mixed-phase stream formed by depressurizing the hot high-separation oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separation gas, the first hot low-separation oil, and the first hot low-separation oil is used as the logistics MCP; the first The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

③The mixed-phase stream formed by depressurizing the hot high-fractionated oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fractionated gas and the first hot low-fractionated oil. The first hot low-fractionated oil is used as the logistics MCP; the first The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

After the first hot low-separation oil is depressurized, it enters the second hot low-pressure flash evaporation process and is separated into the second hot low-separation gas and the second hot low-separation oil. The second hot low-separation oil is used as the logistics MCP; the second hot low-pressure flash evaporation process The operating pressure is greater than atmospheric pressure; the operating pressure of the second hot low-pressure flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

④The mixed-phase stream formed by depressurizing the hot high-fractionated oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fractionated gas and the first hot low-fractionated oil. The first hot low-fractionated oil is used as the logistics MCP; the first The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low-content oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process, and the first negative pressure flash oil is used as the logistics MCP;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

In the second negative pressure flash evaporation process, the base stream MCP-CS is separated into the second negative pressure flash steam and the second negative pressure flash oil; the operating pressure of the second negative pressure flash evaporation process is lower than that of the first negative pressure flash evaporation process. operating pressure;

Separate the condensed oil obtained from the second negative pressure flash steam as quench oil KGS.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is circulating oil;

In the quenching oil supply part K100, the mixed-phase stream formed by depressurizing the hot high-fractionated oil S10-L is used as logistics MCP, and after being mixed with the quenching oil KGS, it becomes the basic logistics MCP-CS;

Quench oil KGS is the condensed oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50;

Quench oil KGS, selected from one or more of the following logistics:

① The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil;

The condensed oil obtained by separating the first hot low-fractionated gas in the separation/fractionation part S50 is used as quenching oil KGS;

② The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low-fragmented gas enters the separation and/or fractionation process of the first hot low-dividing gas for joint recovery;

The condensed oil obtained by separating the first hot low-fractionated gas in the separation/fractionation part S50 is used as quenching oil KGS;

③The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low fraction oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process;

In the separation/fractionation part S50, the condensed oil obtained from the first negative pressure flash steam is separated as quench oil KGS;

④The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low fraction oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process;

The first negative pressure flash oil is separated into a second negative pressure flash steam and a second negative pressure flash oil during the second negative pressure flash evaporation process; the operating pressure of the second negative pressure flash evaporation process is lower than that of the first negative pressure flash evaporation process. operating pressure of the process;

The second negative pressure flash steam enters the separation and/or fractionation process of the first negative pressure flash steam for joint recovery;

The condensed oil obtained from the first negative pressure flash steam is separated in the separation/fractionation section S50 as quench oil KGS.

In the present invention, generally, (6) in the quenching oil supply part K100, the depressurized stream of the hot high-fractionated oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fractionated gas and the first hot low-fractionated oil; The operating pressure of the first hot low-pressure flash evaporation process is greater than the atmospheric pressure; the first hot low-percentage oil is used as the logistics MCP;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

A portion of the base oil-cooled stream obtained from the flash evaporation process based on the base stream MCP-CS is used as quenching oil KGS, which is selected from one or more of the following streams:

① The basic logistics MCP-CS enters the second hot low-pressure flash evaporation process and is separated into the second hot low-pressure flash evaporation process and the second hot low-separated oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low-fragmented gas enters the separation and/or fractionation process of the first hot low-dividing gas for joint recovery;

The condensed oil obtained by separating the first hot low-fractionated gas in the separation/fractionation part S50 is used as quenching oil KGS;

② The basic logistics MCP-CS enters the second hot low-pressure flash process and is separated into the second hot low-separated gas and the second hot low-separated oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low fraction oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process;

The first negative pressure flash steam enters the separation and/or fractionation process of the first negative pressure flash steam for recovery;

The condensed oil obtained from the first negative pressure flash steam is separated in the separation/fractionation section S50 as quench oil KGS.

In the present invention, generally, (2) in the cooling and stabilizing part DT10, the asphaltene-containing stream MCP00 based on the reaction product R10P containing hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C is split into a 2-way stream. MCP01, MCP02, logistics MCP01 is used as the first characteristic logistics to obtain the circulating vacuum flash evaporation oil S50-FL-TOR10, and logistics MCP02 is used as the second characteristic logistics to obtain the external exhaust vacuum flash evaporation bottom oil S50-FL-OUT. logistics;

The first characteristic stream MCP01 is mixed with the first quench oil KGS01 to become the first post-quench mixed stream MCP01-BASE;

Based on the first quenched mixture stream MCP01-BASE, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the first base stream MCP01-CS;

The second characteristic stream MCP02 is mixed with the second quench oil KGS02 to become the second quenched mixed stream MCP02-BASE;

Based on the second quenched mixture stream MCP02-BASE, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the second base stream MCP02-CS;

⑶In the separation/fractionation part S50, after the first base stream MCP01-CS flashes out the first vapor MCP01-CS-FV composed of the low-boiling point component MCP01-LCOM, hydrocarbons containing conventional boiling points higher than 530°C are obtained. The first-pass decompression flash evaporation bottom oil MCP01-S50-FL of the asphaltene-containing solid particle catalyst R10-CAT is a component;

In the separation/fractionation part S50, after the second path basic stream MCP02-CS flashes out the second path vapor MCP02-CS-FV composed of the low-boiling point component MCP02-LCOM, a hydrocarbon group containing a conventional boiling point higher than 530°C is obtained. Second-pass vacuum flash evaporation bottom oil MCP02-S50-FL containing asphaltene-containing solid particle catalyst R10-CAT;

⑷ In the part where the vacuum flash distillation bottom oil is discharged, part or all of the second vacuum flash distillation bottom oil MCP02-S50-FL is used as the discharge vacuum flash distillation bottom oil S50-FL-OUT;

⑸ In the vacuum flash evaporation base oil circulation part, part or all of the first vacuum flash evaporation base oil MCP01-S50-FL is used as circulating vacuum flash evaporation oil MCP01-S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating vacuum flash oil MCP01-S50-FL-TOR10 or the circulating vacuum flash oil MCP01-S50-FL-TOR10 is mixed with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F. touch;

With or without the presence or absence of part of the second decompression flash evaporation base oil MCP02-S50-FL, return to the reaction part R10 to be used as circulating oil MCP02-S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating oil MCP02-S50-FL-TOR10 or the circulating oil MCP02-S50-FL-TOR10 is mixed and contacted with the intermediate hydrogenation product of the heavy oil R10F or the heavy oil R10F;

⑹ In the quenching oil supply part K100, the first quenching oil KGS01 is selected from one or more of the following logistics:

In the quench oil supply section K100, the first quench oil KGS01 is the condensed oil obtained by separating the flash gas of the first basic stream MCP01-CS in the separation/fractionation section S50;

In the quench oil supply section K100, the second quench oil KGS02 is the condensed oil obtained by separating the flash gas of the second basic stream MCP02-CS in the separation/fractionation section S50.

In the present invention, generally, (6) in the quenching oil supply part K100, the first quenching oil KGS01 is the condensed oil obtained in the separation/fractionation part S50 based on the first basic stream MCP01-CS flash gas, and is selected from one of the following streams One or more species:

① Mainly composed of heavy diesel components and containing waxy oil components, coming from the positive pressure fractionation process based on the first basic stream MCP01-CS flash gas;

② Mainly composed of wax oil components with conventional boiling points lower than 430°C, derived from the negative pressure fractionation process based on the first basic stream MCP01-CS flash gas;

In the quenching oil supply section K100, the second quenching oil KGS02 is the condensed oil obtained in the separation/fractionation section S50 based on the second basic stream MCP02-CS flash gas, and is selected from one or more of the following streams:

① Mainly composed of heavy diesel components and containing waxy oil components, coming from the positive pressure fractionation process based on the second basic stream MCP02-CS flash gas;

② Mainly composed of wax oil components with conventional boiling points lower than 430°C, derived from the negative pressure fractionation process based on the second basic stream MCP02-CS flash gas.

In the present invention, generally, (3) in the separation/fractionation part S50, the second path basic stream MCP02-CS flashes out the low boiling point component MCP02-LCOM and the second path vapor MCP02-CS-FV separation and recovery system MCP02-CS -FV-SYS, separate and recovery system MCP01-CS-FV-SYS for the first vapor MCP01-CS-FV consisting of the first basic stream MCP01-CS that flashes out the low-boiling component MCP01-LCOM, respectively. Set up or jointly set up to share at least part of the system.

In the present invention, usually, (3) in the separation/fractionation part S50, the first characteristic stream MCP01 enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fraction gas and the first hot low-fraction gas. Oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-separation oil in the first path is depressurized and then enters the second hot low-pressure flash evaporation process in the first path and is separated into the second hot low-separation gas in the first path, the second hot low-separation oil in the first path; the second hot low-separation oil in the first path; The operating pressure of the thermal low-pressure flash evaporation process is greater than the atmospheric pressure; the operating pressure of the first and second thermal low-pressure flash evaporation processes is lower than the operating pressure of the first and first thermal low-pressure flash evaporation processes;

The first second hot low fraction oil is separated into the first first negative pressure flash steam and the first negative pressure flash oil in the first negative pressure flash evaporation process;

In the separation/fractionation part S50, the second characteristic stream MCP02 enters the first hot low-pressure flash evaporation process of the second path and is separated into the first hot low-fragmented gas of the second path and the first hot low-fragmented oil of the second path; 1. The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-fractionated oil in the second path is depressurized and enters the second hot low-pressure flash evaporation process in the second path and is separated into the second hot low-percentage gas in the second path, the second hot low-percentage oil in the second path; the second hot low-percentage oil in the second path; The operating pressure of the hot low-pressure flash evaporation process is greater than the atmospheric pressure; the operating pressure of the second hot low-pressure flash evaporation process of the second path is lower than the operating pressure of the first hot low-pressure flash evaporation process of the second path;

The second hot low-carbon oil in the second path is separated into the first negative pressure flash steam in the second path and the first negative pressure flash oil in the second path during the first negative pressure flash evaporation process in the second path;

The second hot low-fragmented gas and the first hot low-fragmented gas of the first path are mixed and separated in the first hot low-divided gas separation and recovery system;

The second hot low-fractionated gas from the second path and the second hot low-fragmented gas from the first path are mixed and separated in the second hot low-fractionated gas separation and recovery system;

The first negative pressure flash steam from the first channel and the first negative pressure flash steam from the second channel are mixed and separated in the first negative pressure flash steam separation and recovery system.

In the present invention, usually, the second first hot low-pressure flash evaporation process and the first first hot low-pressure flash evaporation process are carried out in different spaces separated by partition plates in the pressure-bearing shell of the same container. The vapor phase space of the first hot low-pressure flash evaporation process is connected with the vapor phase space of the first hot low-pressure flash evaporation process;

The second hot low-pressure flash evaporation process of the second pass and the second hot low-pressure flash evaporation process of the first pass are carried out in different spaces separated by partition plates in the pressure shell of the same vessel. The second hot low-pressure flash evaporation process of the second pass The vapor phase space of the process is connected with the vapor phase space of the first and second hot low-pressure flash evaporation process;

The second first negative pressure flash evaporation process and the first first negative pressure flash evaporation process are carried out in different spaces separated by partition plates in the shell of the same container that bears negative pressure. The second first negative pressure flash evaporation process is The vapor phase space of the flash evaporation process is connected with the vapor phase space of the first negative pressure flash evaporation process.

In the present invention, usually, (3) in the separation/fractionation part S50, in the positive pressure separation process, the base stream MCP-CS is separated into hot low-fractionated gas and hot low-fragmented oil;

The condensed oil obtained by separating the first hot low-component gas is used as quenching oil KGS;

The way to separate the first hot low-component gas is to use the rectification section T11. The first hot low-component gas enters the lower part of the rectification section T11 and flows from bottom to upward along the rectification section T11 to fractionate the product: the bottom oil of the rectification section T11. , at least part of it is used as the logistics of quenching oil KGS, 1 or 2 or more lines of gas oil, and tower top exhaust gas;

Distillation section T11 uses oil-cooled reflux extracted from the middle section and/or cold circulation cold reflux at the top of the tower and/or cold reflux at the top of the tower to create a mass transfer liquid phase;

The hydrocarbon stream with or without a waxy oil component based on cold high-fractionated oil, which mainly consists of diesel components, enters the distillation section T11 for joint recovery.

In the present invention, generally, a hydrocarbon stream with or without a waxy oil component based mainly on a diesel component based on cold high-fractionated oil enters the distillation section T11 above the extraction port of the distillate used as quench oil KGS , the location of the tower section below the gas oil extraction outlet.

In the present invention, generally, the gas oil enters the gas diesel light component removal tower and is separated into the bottom diesel oil of the gas diesel light component removal tower and the top gas of the gas diesel light component removal tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T11.

In the present invention, two or more channels of gas oil from the distillation section T11 can enter the same gas diesel light component removal tower and be separated into the bottom diesel oil of the gas diesel light component removal tower and the gas oil light component removal tower air at the top of the tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T11.

In the present invention, usually, the operating pressure of the reflux tank of the gas oil light component removal tower is 0.105-0.5MPa (absolute pressure).

In the present invention, usually, (3) in the separation/fractionation part S50, in the positive pressure separation process, the base stream MCP-CS is separated into hot low-fractionated gas and hot low-fractionated oil; in the negative pressure separation process, the hot low-fractionated oil is separated into Negative pressure flash steam, negative pressure flash evaporation base oil;

The condensed oil obtained by separating the negative pressure flash steam is used as quench oil KGS;

The way to separate the negative pressure flash steam is to use the negative pressure rectification section T22. The negative pressure flash steam enters the lower part of the negative pressure rectification section T22 and flows from bottom to upward along the rectification section T22 to fractionate the product: bottom oil in the rectification section T22. , at least part of it is used as the logistics and tower top exhaust gas of quenching oil KGS;

The distillation section T22 uses the oil-cooled reflux extracted from the middle section and/or the cold circulation cold reflux at the top of the tower and/or the cold reflux at the top of the tower to create the mass transfer liquid phase;

The hydrocarbon stream with or without a waxy oil component based on cold high-fractionated oil, which mainly consists of diesel components, enters the distillation section T22 for joint recovery.

In the present invention, generally, a hydrocarbon stream with or without a waxy oil component based on cold high-fractionated oil, mainly composed of diesel components, enters the distillation section T22 above the extraction port of the distillate used as quench oil KGS , the location of the tower section below the gas oil extraction outlet.

In the present invention, generally, the gas oil enters the gas diesel light component removal tower and is separated into the bottom diesel oil of the gas diesel light component removal tower and the top gas of the gas diesel light component removal tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T22.

In the present invention, two or more channels of gas oil from the rectification section T22 can enter the same gas diesel light component removal tower and be separated into the bottom diesel oil of the gas diesel light component removal tower and the gas oil light component removal tower air at the top of the tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T22.

In the present invention, usually, the operating pressure of the reflux tank of the gas oil light component removal tower is 0.105-0.5MPa (absolute pressure).

In the present invention, generally, the use of T22 base oil in the rectification section is selected from one or more of the following:

① Return to the R10 cycle reaction of the reaction part of heavy oil suspended bed hydrogenation conversion;

② Inside the distillation section T22, it directly enters the negative pressure flash evaporation bottom oil without passing through the oil collection tank;

③After mixing with a part of the negative pressure flash evaporation base oil, return to the reaction part R10 of the heavy oil suspension bed hydrogenation conversion for cycle reaction.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is a hydrocarbon oil rich in aromatics, and more than 80% of the quenching oil KGS is vaporized in the separation/fractionation part S50 and enters the flash gas of the basic stream MCP-CS , thereby bringing the heat absorbed in the cooling stabilization part DT10 into the flash gas of the basic stream MCP-CS for utilization. During the condensation process of the flash gas of the basic stream MCP-CS, the gas phase components from the quenching oil KGS More than 80% complete the condensation process to release heat.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is a hydrocarbon oil rich in aromatics, and more than 95% of the quenching oil KGS is vaporized in the separation/fractionation part S50 and enters the flash steam of the basic stream MCP-CS In the body, the heat absorbed in the cooling stabilization part DT10 is brought into the flash gas of the basic stream MCP-CS and utilized. During the condensation process of the flash gas of the basic stream MCP-CS, the gas phase group from the quenching oil KGS More than 95% of the condensation process is completed to release heat.

Detailed ways

The present invention is described in detail below.

The pressure mentioned in the present invention refers to absolute pressure.

The conventional boiling point mentioned in the present invention refers to the vapor and liquid equilibrium temperature of a substance under one atmospheric pressure.

The normal boiling range mentioned in the present invention refers to the normal boiling point range of the fraction.

The specific gravity mentioned in the present invention, unless otherwise specified, refers to the ratio of the density of liquid under normal pressure and 15.6°C to the density of water under normal pressure and 15.6°C.

Unless otherwise specified, the composition, concentration, content or yield value of the components described in the present invention are based on weight.

The conventional gaseous hydrocarbons mentioned in the present invention refer to hydrocarbons in gaseous state under normal conditions, including methane, ethane, propane, and butane.

The conventional liquid hydrocarbons described in the present invention refer to hydrocarbons that are liquid under normal conditions, including pentane and hydrocarbons with higher boiling points.

The impurity elements mentioned in the present invention refer to non-hydrogen, non-carbon, and non-metal components in the raw oil, such as oxygen, sulfur, nitrogen, chlorine, etc.

The impurity components mentioned in the present invention refer to the hydrogenation conversion products of non-hydrocarbon components in the raw oil, such as water, ammonia, hydrogen sulfide, hydrogen chloride, etc.

The naphtha component of the present invention refers to conventional liquid hydrocarbons with conventional boiling points lower than 180°C.

The diesel component of the present invention refers to hydrocarbons with a conventional boiling point of 180 to 350°C.

The wax oil component of the present invention refers to hydrocarbons with a conventional boiling point of 350 to 530°C.

The residual oil component in the present invention refers to hydrocarbons with a conventional boiling point higher than 530°C.

The light hydrocarbons described in the present invention refer to naphtha components and hydrocarbons with lower boiling points.

The hydrogen-to-oil volume ratio in the present invention refers to the ratio of the standard state volume flow rate of hydrogen to the volume flow rate of the specified oil stream at normal pressure and 20°C.

The gravimetric chemical hydrogen consumption during the hydrogenation reaction of heavy oil R10F according to the present invention refers to the weight of hydrogen consumed for chemical reaction per unit weight of heavy oil R10F during the hydrogenation reaction, for example, 2.00%.

In the heavy oil suspended bed hydrogenation reaction process of the present invention, the gas-liquid contact method in the suspended bed hydrogenation reactor is not limited and can be any effective method.

In the heavy oil suspended bed hydrogenation reaction process of the present invention, the granular heavy oil suspended bed hydrogenation catalyst used in the reaction process is suspended in the liquid phase of the reaction process to form an oil slurry with catalyst particles dispersed, so it can also be called heavy oil slurry. state bed hydrogenation reaction process.

In the heavy oil suspended bed hydrogenation reaction process of the present invention, the suspended bed hydrogenation reactor is usually an upflow hydrogenation reactor, and the dominant direction of the macroscopic flow of the process medium in the reaction space or hydrogenation catalyst bed is from the bottom to the bottom. up.

The upflow suspended bed reactor of the present invention belongs to the upflow expanded bed reactor.

The upflow expanded bed reactor of the present invention is a vertical upflow reactor, which is an expanded bed catalytic reactor when a catalyst is used; the vertical type refers to the central axis of the reactor in the working state after installation being perpendicular to the ground; the upflow type refers to The main flow direction of the material in the reaction process is from bottom to top through the reaction space or catalyst bed or in the same direction as the upward catalyst; the expanded bed refers to the working state of the catalyst bed in an expanded state, and the catalyst bed expansion ratio is defined as the catalyst bed The ratio KBED of the maximum height CWH of the working state when the reaction raw material passes through the catalyst bed to the height CUH of the empty bed of the catalyst bed. Usually, when KBED is lower than 1.10, it is called a micro-expansion bed, and KBED is between 1.25 and 1.55. is called an ebullating bed, while a suspended bed is considered the most extreme form of an expanded bed.

The backmixed flow expanded bed reaction zone of the present invention refers to the operating mode of the reaction zone using an expanded bed reactor, where liquid flow backmixing or circulating liquid exists; the backmixed flow or circulating liquid refers to the flow at process point K At least a part of the liquid phase XK-L in the intermediate product XK or the final product XK is returned to the reaction zone upstream of the stream XK as a circulating liquid stream XK-LR. The reaction product of the circulating liquid stream XKLR flows through point K and exists in XK. The method of forming the backmixed flow can be any suitable method, such as setting up a built-in inner circulation tube, a built-in external circulation tube, a built-in liquid collection cup + diversion tube + circulation pump, an external circulation tube, etc.

The liquid collecting cup or liquid collector provided in the reactor of the present invention refers to a container arranged in the reactor for collecting liquid. Usually the upper or upper side is open, and the bottom or lower side is equipped with a guide pipe for discharge. Collect liquid; the top liquid collector of the expanded bed reactor is usually installed in the deliquidating area of gas and liquid materials to obtain liquid and gas-liquid mixed phase streams or liquid and gas.

The structural form of the suspended bed reactor of the present invention can be any suitable form. It can be an empty cylinder suspended bed reactor to form a plug flow or a backmixed flow with internal circulation. It can be an internal circulation guide tube to form a plug flow. To form an internal internal circulation flow or an internal external circulation flow, the external circulation pipe can be used to flow the upper reaction space liquid into the lower reaction space to form a back-mixed flow type of the external circulation flow of the device, or the top product liquid collection and diversion system can be used to pass the circulation The pressurized system forms a back-mixed flow pattern of forced internal circulation flow.

The thermal polymerizer of the present invention refers to a gas-liquid separation device used to separate intermediate products or final products of hydrogenation reactions.

The working mode of the suspended bed hydrogenation reactor of the present invention can be selected:

①Suspended bed hydrogenation reactor;

② The combined bed hydrogenation reactor of suspended bed and ebullating bed can unload the ebullated bed catalyst whose activity has been reduced from the bottom of the bed in an intermittent manner, and replenish the fresh ebullating bed catalyst from the upper part of the bed in an intermittent manner to maintain the bed. Layer ebullating bed catalyst storage capacity.

The raw material heavy oil R10F in the heavy oil suspended bed hydrocracking reaction process of the present invention usually refers to asphaltene-containing hydrocarbon oil mainly (weight concentration greater than 50%) composed of hydrocarbon components with conventional boiling points higher than 530°C, such as Pressure residue oil, atmospheric pressure residue oil and a mixture of several hydrocarbon materials; when heavy oil R10F is mixed from several branch feed oils with different properties, at least one branch feed oil contains asphaltenes, and the other one or Several branch feed oils contain asphaltenes or do not contain asphaltenes.

The heavy oil suspended bed hydrocracking reaction process R10 of the present invention usually refers to the suspended bed hydrocracking reaction process of vacuum residue oil, and its purpose is to achieve as much as possible the hydrocarbon components in the heavy oil R10F with a conventional boiling point higher than 530°C. A high cracking conversion rate (the cracking conversion rate is usually expected to be greater than 90% or 95% by weight) means to minimize the ratio of hydrocarbon components with a conventional boiling point higher than 530°C in the discharged unconverted oil, while maximizing the recovery and utilization of heat energy. efficiency, reducing the amount of catalyst; of course, the heavy oil suspension bed hydrocracking reaction process of the present invention also includes other heavy oil suspensions that produce easily thermally condensable hydrocarbon components at high temperatures in addition to the vacuum residue suspension bed hydrocracking reaction process. Bed hydroconversion reaction process.

Usually, in order to ensure the relative economic competitiveness of different types of heavy oil hydrogenation reaction processes, the raw material vacuum residue in the ebullating bed hydrocracking process (containing 85 to 90% of the vacuum residue components and the residual carbon content is usually 18 to 18%). 23% by weight) has more stringent properties than the feed oil of VRDS in the fixed-bed hydrodesulfurization process (containing 55-65% vacuum residue components, and the residual carbon content is usually 9-14% by weight), while the suspended bed hydrodesulfurization process The raw material vacuum residue in the hydrocracking reaction process (containing 90 to 95% vacuum residue components, and the residual carbon content is usually 22 to 33% by weight) has better properties than the raw material vacuum residue in the ebullating bed hydrocracking process. are more demanding in nature.

The asphaltene content of vacuum residue, the raw material for the suspended bed hydrocracking reaction process, is usually higher than 12%, generally higher than 18%, especially higher than 22%, and its Conian carbon residue value is usually higher than 16%, generally higher than 16%. Higher than 27%, especially higher than 33%, its organic sulfur content is usually higher than 0.5%, generally higher than 2.0%, especially higher than 5.0%, and its organic nitrogen content is usually higher than 0.15%, generally higher than 0.30% , especially higher than 0.50%, and its organometallic content is usually higher than 0.015%, generally higher than 0.025%, especially higher than 0.100%.

The oil produced by the heavy oil suspended bed hydrocracking in the present invention refers to the hydrocarbon oil stream mainly composed of conventional liquid hydrocarbons based on the heavy oil suspended bed hydrocracking reaction product; the oil produced by the heavy oil suspended bed hydrocracking can be 1, Two or more hydrocarbon streams, usually at least one hydrocarbon stream in the oil produced by heavy oil suspension bed hydrocracking contains asphaltene components. These streams are usually separated into gases and hydrocarbon fractions with different boiling ranges after flash evaporation and fractionation steps. Base oil composed of oil-releasing, non-evaporating components.

The bottom oil in the present invention refers to the hydrocarbon liquid composed of non-evaporable hydrocarbon oil components after the flash evaporation and fractionation steps.

The stable cooling of the oil produced by heavy oil suspended bed hydrocracking in the present invention refers to the large-span cooling process of the oil produced by heavy oil suspended bed hydrocracking during the separation and fractionation process. This cooling process is not mainly due to the temperature drop caused by depressurization and evaporation. , but is a restrictive cooling mainly adopted to achieve thermal stabilization of the asphaltene component in the liquid phase. The reason is that asphaltene in the oil produced by heavy oil suspension bed hydrocracking will occur at high temperatures (such as ≥380°C). Thermal condensation reactions generate thermal condensates. Once the concentration of these thermal condensates exceeds the upper limit of solubility, they will be freed from the main solution and aggregate into the second liquid phase, the asphaltene phase, and generate thermal condensates such as soft coke or coke. The accumulation of sediments will As a result, the fractionation system is forced to shut down; for the heavy oil suspended bed hydrocracking process of the cycle conversion type, especially the large cycle ratio cycle conversion type, the oil separation and fractionation process continuously produces thermal condensates, which will lead to the asphaltene in the reactor solution. The circulation accumulation increases. In order to maintain the stability of the asphaltene solution in the fresh heavy oil reaction process (ie, limit the asphaltene concentration value to be lower than the safe concentration value), this will essentially limit the single-pass conversion rate of the fresh heavy oil in the suspended bed hydrocracking reaction process. , total conversion rate. In fact, whether it is the hydrocracking reaction process of heavy oil in a suspended bed or the separation and fractionation process of oil produced by hydrocracking of heavy oil in a suspended bed, the stability of the asphaltene solution is the first condition that must be ensured to maintain long-term stable operation.

In the heavy oil suspended bed hydrocracking reaction process, since the non-asphaltene components in the raw material vacuum residual oil are more susceptible to hydrocracking than the asphaltene components, the suspended bed hydrocracking reaction process of vacuum residual oil must be It causes the concentration of asphaltene in the unconverted oil, which means that the properties of the bottom oil of the vacuum tower with the same boiling range are much worse than the properties of the raw material vacuum residue with the same boiling range. The large circulation ratio operation mode of unconverted oil is adopted. The solution properties of the initial reaction process (relatively high asphaltene concentration) are much worse than those of the simple single-pass operation mode of fresh vacuum residue (relatively low asphaltene concentration); on the other hand, using unconverted oil The solution properties of the final reaction process in the operation mode with large circulation ratio and low single-pass conversion rate of residue reduction components (high concentration of aromatic components in the solution and better solubility of asphaltene) are better than those of pure fresh vacuum residue oil in one pass. , the solution properties of the final reaction process in the high conversion rate operation mode (low concentration of aromatic components in the solution, poor solubility of asphaltene) are better.

A large amount of experimental data and production operation data show that even if a nanoscale molybdenum-based catalyst with excellent hydrogenation performance is used, such as the EST vacuum residue suspended bed hydrocracking process of Italian ENI Company, which adopts a mild reaction temperature vacuum residue The suspended bed hydrocracking process of oil is carried out under the conditions of reaction operating pressure of 16 to 17MPa, operating temperature of 420 to 440°C, circulating tail oil weight ratio of 100 to 150%, and the overall conversion rate of fresh vacuum residue oil to 88 to 95%. The asphaltene concentration in the tail oil is also 120 to 160% or higher of that of fresh vacuum residue, and the carbon residue value of the tail oil is 160 to 200% or higher of that of fresh vacuum residue. The carbon residue of the tail oil The ratio of the value to the residual carbon value of the fresh vacuum residue is higher than the ratio of the asphaltene concentration of the tail oil to the asphaltene concentration of the fresh vacuum residue. This is the contribution of macromolecular olefins, and the thermal stability of macromolecular olefins and asphaltenes The properties are very poor, that is, thermal condensation reactions will occur at high temperatures (such as ≥380°C) to form thermal condensates.

Usually, the heavy oil suspended bed hydrocracking process of the present invention uses heavy oil suspended bed hydrocracking molybdenum catalyst particles in the form of MOS _2. Due to the characteristics of thermal cracking and the relatively low hydrogenation saturation rate relative to the thermal cracking speed, a large number of The presence of unsaturated olefins will inevitably cause the thermal condensation of some asphaltenes to form macromolecular thermal condensates with lower hydrogen content and more difficult to hydrogenate and thermally crack. They will occur at high temperatures and in an environment where hydrogen is lost. Thermal condensation reaction has been verified by experiments, which is the theoretical basis for the oil produced by heavy oil suspension bed hydrocracking described in the present invention to be stabilized by cooling.

The EST residue suspension bed hydrocracking process of Italian Eni Company, because the tail oil contains a large amount of macromolecular olefins, inferior asphaltene and other components with poor thermal stability, they will produce thermal condensation products at high temperatures and lose hydrogen at the same time. After partial pressure protection, metal sulfides (impurity metal compounds, catalyst molybdenum sulfide) all have a certain degree of thermal cracking catalysis to promote the generation of thermal condensates, and also aggravate the generation of thermal condensates. Therefore, the heat after decompression is high. The separation and fractionation process of oil separation is not only a physical process, but also a chemical process in which a certain number of thermal condensation reactions occur at high temperatures. In an operation method with a large amount of circulating tail oil, these heat shrinkage products are in the fractionation process and reaction The process gradually accumulates. Part of it is discharged from the device with the external tail oil, and most of it accumulates in the reaction and fractionation systems through circulating tail oil, which will gradually deteriorate the liquid phase properties of the reaction system and fractionation system. Ultimately, in order to control the liquid phase properties of the reaction system and fractionation system, Stable phase properties (limiting the asphaltene concentration to be lower than the safe value) are forced to reduce the single-pass conversion rate and overall conversion rate of fresh vacuum residue reaction raw materials.

As mentioned above, the overall conversion rate of vacuum residual oil in the vacuum residual oil suspended bed hydrocracking unit is not only affected by the essential conversion rate of the reaction process, but also by the oil separation process produced by suspended bed hydrocracking (especially vacuum distillation Process) The thermal stability of the separation bottom oil (concentrated asphaltene liquid phase) is affected (correlated with the thermal condensate production during the separation and fractionation process), and is also affected by the asphaltene concentration (heavy wax) of the circulating tail oil generated by the suspension bed hydrocracking process of the oil separation process. Oil extraction rate) (correlated with the asphaltene concentration of the circulating oil, the concentration of the asphaltene solvent, and the output tail oil yield), and the above two factors are coupled with each other in the conventional single fractionation process.

When the stability of the asphaltene solution produced by suspended bed hydrocracking in the oil separation process is threatened (shown as coking in the hot low-pressure separator, coking at the bottom of the atmospheric tower, and coking at the bottom of the vacuum tower), in order to maintain continuous operation, only can be forced to reduce the conversion rate of the reaction process, which will increase the proportion of unconverted oil discharged (that is, increase the yield of vacuum distillation bottom oil and reduce the catalyst concentration), and subsequently reduce the proportion of circulating oil carrying catalyst, which will increase The consumption of fresh catalyst or its precursor may be forced to increase the amount of circulating oil and reduce the processing load.

Conversely, from the perspective of optimizing process operations, if the stability of the asphaltene solution in the oil separation process produced by suspended bed hydrocracking can be improved and the output of thermal condensates can be reduced, it will be beneficial to extend the continuous operation cycle, improve the conversion rate of the reaction process, and Reduce the proportion of unconverted oil discharged (that is, reduce the yield of vacuum distillation bottom oil and increase the catalyst concentration), thereby increasing the proportion of circulating oil carrying catalyst, which can reduce the consumption of fresh catalyst or its precursor, and It can reduce the amount of circulating oil and increase the processing capacity of the device.

The above analysis is a conclusion based on experimental research and production experience. Therefore, in order to improve the thermal stability of the oil produced by heavy oil suspension bed hydrocracking, it is necessary to reduce the operation of the heat-sensitive liquid phase containing asphaltenes in the separation and fractionation process. temperature.

After the cooling is implemented to improve the thermal stability of the oil produced by heavy oil suspended bed hydrocracking, it will inevitably lead to the removal or transfer of the heat energy carried by the oil produced by heavy oil suspended bed hydrocracking. The utilization of these heat energy will inevitably be affected by the "heavy oil suspended bed hydrocracking" The effect of cooling the generated oil and stabilizing the operating mode.

In the fractionation process, the circulating oil in the hot high-fractionated oil has three functions. On the one hand, the circulating oil is a huge heat carrier. After the reaction belt is taken out of the reactor, it releases heat during the stabilization and cooling process during the separation and fractionation processes. On the other hand, it releases heat during the depressurization flash evaporation process of the fractionation process; on the other hand, it acts as an asphaltene stabilizing solvent during the heavy oil suspended bed hydrogenation conversion reaction process in the reactor, that is, reducing the single-pass conversion rate and reducing the reactor The concentration of asphaltenes in the liquid phase at the outlet increases the concentration of colloids and heavy aromatics in the liquid phase at the outlet of the reactor;

In fact, since the circulating oil essentially does not evaporate during the reaction and fractionation processes, the outlet operating temperature of the heavy oil suspended bed hydroconversion reactor is very high (such as 420-440°C), while the temperature of the flash section of the vacuum tower is relatively low (such as 340~360℃), the temperature difference between the two is about 60~90℃. In this way, the circulating oil plays the role of a liquid heat carrier that brings out a large amount of reaction heat. Usually, the weight flow rate of the circulating oil is slightly greater than the weight flow rate of the raw oil (or the net production Oil weight flow rate), therefore, the circulating oil carries a huge amount of reaction heat and is a huge heat reservoir, which essentially plays the following three roles in the fractionation part:

First, the large amount of heat energy transferred from the net reaction-generated oil in the hot high-fractionation oil during the stabilization and cooling process is given as an exothermic feedback during the evaporation endothermic step of the separation and fractionation process, thereby improving the equilibrium flash evaporation of the separation and fractionation process. temperature, which is conducive to improving the pullout rate;

Second, it is used to balance the large amount of heat absorbed by the net reaction in the high-fractionated oil during the fractionation evaporation process. It can reduce the equilibrium temperature of the flash evaporation step under the same flash steam extraction rate, which is beneficial to improving the thermal stability of the base oil. ;

Third, there is still a large amount of heat energy that needs to be recovered. The temperature of this heat energy is between the thermal high temperature (such as 420~440℃) and the stabilization temperature (such as 380~390℃). In other words, how to reasonably The problem of recovering these high-temperature thermal energy.

CN115975675A discloses a heavy oil suspended bed hydroconversion method. The oil KP produced by the reaction is injected with quenching oil to mix and cool down stably. It is suitable for the vacuum residual oil suspension bed hydrocracking process with a large circulation ratio of circulating oil. The quenching oil is selected from Compared with the cooling method of KP indirect heat exchange to transfer heat, the advantages of hydrocarbon oil containing reaction raw material heavy oil components and low boiling point components, reaction raw material heavy oil, and bottom oil separated by KP are: ① KP achieves rapid cooling; ② quenching oil The heat released during the subsequent evaporation process of KP can increase the extraction rate, the flow adjustment is flexible, and the temperature of the heat energy after final recovery is high; ③ External quenching oil can reduce the asphaltene concentration in the base oil; ④ The circulating quenching oil can transfer heat at a stable temperature and can Flexibly supply heat to multiple points; ⑤ The generated oil branch is operated with different quenching oil cooling distillations, which can reduce the output tail oil yield, improve the heat recovery efficiency, improve the reaction conversion rate, and form a combined distillation of crude oil, inverted preheating of reaction raw materials, During normal operation, there is no oil heating furnace heating and other processes. CN115975675A A heavy oil suspended bed hydrogenation conversion method document records the heavy oil and heavy oil suspended bed hydrogenation conversion reaction conditions (reaction temperature, reaction pressure, circulating oil circulation ratio, heavy oil suspended bed hydrogenation conversion reaction process involved) Hydrogen conversion catalyst and its dosage), heavy oil conversion rate, and separation and fractionation method of oil produced by heavy oil suspended bed hydrogenation conversion reaction.

The present invention can construct a combined distillation process for mixed oil containing diesel and wax oil components. It is a heat-carrying fractionation path different from the heat-carrying low-fractionated oil to the vacuum distillation process S02, and avoids the need for decompression. The large amount of circulation of the bottom oil in the pressure tower reduces the liquid phase concentration of distillate oils such as wax oil in the thermal low-fractionated oil.

The low-grade medium-temperature heat in the present invention refers to the medium-temperature heat with a lower temperature, and the high-grade medium-temperature heat refers to the medium-temperature heat with a higher temperature. There is a relative relationship between the two.

The present invention can jointly fractionate hydrocarbon streams containing diesel and wax oil components based on cold high-fractionated oil. It can be any suitable process. Generally, cold high-fractionated oil, especially cold high-fractionated oil, removes conventional gaseous hydrocarbons or light The light-component hydrocarbon material obtained after naphtha or heavy naphtha components can enter the separation and/or distillation process S01 of hot low-fractionated gas or the vacuum flash steam based on the thermal low-fractionated oil stream. The S02 joint fractionation of the distillation section serves as the cold reflux liquid in the fractionation section, saving unnecessary preheating and temperature rise of the fractionated raw material hydrocarbons and cooling of the circulating oil in the middle section of the fractionation tower, simplifying the process; at the same time, cold high-fractionated oil and cold high-fractionated oil-based The heating process of the light component hydrocarbon stream can be used as a cold source to recover the separation and/or distillation process of hot low-fractionated gas S01, and the middle of the rectification section S02 of the vacuum flash steam based on the hot low-fractionated oil stream. Warm heat (such as condensation and cooling of hot low fractions, heat release in the condensation and cooling process of fractionation tower overhead gas, and reflux heat in the middle of the fractionation tower).

Features of the present invention are described below.

The tail oil circulation type heavy oil suspension bed hydrocracking product thermal high-fractionation oil cooling and separation method of the present invention is characterized by:

The heavy oil suspended bed hydroconversion process U100 for converting heavy oil into low molecular weight hydrocarbons includes a reaction part R10 for carrying out heavy oil suspended bed hydroconversion, a hydrocarbon component with a conventional boiling point lower than 530°C based on the reaction product R10P and a conventional boiling point higher than 530℃ hydrocarbon component asphaltene-containing stream MCP injection quench oil KGS cooling stabilization part DT10, basic stream MCP-CS separation/fractionation part S50, vacuum flash bottom oil discharge part, vacuum flash bottom Oil circulation part and quenching oil supply part K100;

In the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in heavy oil R10F is greater than 30%;

⑴ In the reaction part R10 of heavy oil suspended bed hydrogenation conversion, in the presence of hydrogen, conventional liquid hydrocarbons, and the solid particle catalyst R10-CAT for heavy oil suspended bed hydrogenation conversion, there is or is not the presence of hydrogen-donating hydrocarbons, and the presence or absence of other solid particles. Under the condition of miscible materials, heavy oil R10F and circulating vacuum flash oil S50-FL-TOR10 from the vacuum flash bottom oil circulation part are converted into heavy oil suspension bed hydrogenation conversion reaction R10R including suspension bed hydrocracking reaction. Product R10P;

The solid particle catalyst R10-CAT contains at least Mo element, and the main working form of Mo in the reaction part R10 is M0S2;

Heavy oil R10F, whose conventional boiling point is higher than 530°C and the weight concentration of hydrocarbon components is greater than 50%, contains one or more impurity components such as asphaltenes, organic sulfur, organic nitrogen, and organic metals;

Heavy oil R10F is used as the fresh reaction feed of the reaction part R10, which is a mixed raw material of a single property of raw oil or several different properties of branch raw materials;

When heavy oil R10F is mixed from several split feed oils with different properties, at least one split feed oil contains asphaltenes, and one or several other split feed oils may or may not contain asphaltenes;

The heavy oil suspended bed hydroconversion reaction R10R includes a suspended bed hydrocracking reaction, which allows at least a part of the hydrocarbon components in the heavy oil R10F with a conventional boiling point higher than 530°C to complete the hydrocracking reaction and convert it into hydrocarbon products with smaller molecular weights;

The heavy oil suspended bed hydroconversion reaction R10R includes a suspended bed hydrofinishing reaction, which enables at least a part of the impurity elements in the heavy oil R10F to complete a hydrogenation and deimpurity reaction, and makes at least a part of the unsaturated carbon-carbon bonds of at least a part of the hydrocarbon components in the heavy oil R10F Be saturated with hydrogenation; the hydrogenation and impurity removal reaction includes one or more of a hydrodemetallization reaction, a hydrodesulfurization reaction, a hydrodenitrification reaction, and a hydrodeoxygenation reaction;

The average asphaltene weight concentration of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average asphaltene weight concentration of the heavy oil R10F;

The average Conian carbon residue value of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average Conian carbon residue value of heavy oil R10F;

The average organic sulfur weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average organic sulfur weight content of heavy oil R10F;

The average organic nitrogen weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average organic nitrogen weight content of heavy oil R10F;

The average organic metal weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average organic metal weight content of heavy oil R10F;

In the hot high-pressure separation part S10, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C based on the reaction product R10P is separated into hot high-fractionated gas S10-V and hot high-fractionated oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quench oil KGS to become a post-quench mixture. LogisticsMCP-BASE;

An asphaltene-containing stream based on the quenched mixture stream MCP-BASE containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the base stream MCP-CS;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash distillation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in the external discharge vacuum flash evaporation bottom oil S50-FL-OUT is lower than 70% of the weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in heavy oil R10F. %;

⑸ In the vacuum flash evaporation bottom oil circulation part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash evaporation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is returned to the reaction part R10 as circulating vacuum flash oil S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating vacuum flash oil S50-FL-TOR10 or the circulating vacuum flash oil S50-FL-TOR10 is mixed and contacted with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F;

⑹ In the quenching oil supply part K100, the quenching oil KGS is a hydrocarbon oil rich in aromatics, and most of the quenching oil KGS vaporizes in the separation/fractionation part S50 and enters the flash gas of the basic stream MCP-CS, which will be cooled during the cooling process. The heat absorbed by the stabilizing part DT10 is brought into the flash gas of the basic stream MCP-CS and utilized. During the condensation process of the flash gas of the basic stream MCP-CS, most of the vapor phase components from the quench oil KGS complete the condensation process. Release heat.

According to the present invention, generally, in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F is greater than 50%;

⑴ In the reaction part R10 of the heavy oil suspended bed hydrogenation conversion, the heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 70%, and at least one of the following conditions is met:

① Asphaltene weight concentration is greater than 12%;

②Kang’s carbon residue value is higher than 16%;

③The weight content of organic sulfur is higher than 0.5%;

④The weight content of organic nitrogen is higher than 0.15%;

⑤The organic metal weight content is higher than 0.015%;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

In the cooling stabilization part DT10, the logistics MCP with a temperature of T1 is mixed with the quenching oil KGS with a temperature of T3 to become a quenched mixed flow MCP-BASE with a temperature of T2. The cooling range of the logistics MCP is DT, DT=T1-T2, DT 15～80℃;

Logistics MCP is selected from one or more of the following logistics:

①The reaction product R10P is used as logistics MCP;

②Thermal high-percentage oil S10-L is used as logistics MCP;

③The vapor-liquid miscible material formed by hot high-percentage oil S10-L after decompression is used as logistics MCP;

④The vapor-liquid miscible material formed by the hot high-fragment oil S10-L after decompression is separated into first-level hot low-pressure flash steam and first-level hot low-pressure flash oil in the first-level hot low-pressure flash evaporation process; the first-level hot low-pressure flash evaporation process The operating pressure is greater than atmospheric pressure;

First-grade hot low-pressure flash oil, used as logistics MCP;

⑤The vapor-liquid miscible material formed by the hot high-fraction oil S10-L after decompression is separated into first-level hot low-pressure flash steam and first-level hot low-pressure flash oil in the first-level hot low-pressure flash evaporation process; the first-level hot low-pressure flash evaporation process The operating pressure is greater than atmospheric pressure;

After the pressure of the primary hot low-pressure flash oil is reduced, it is separated into secondary hot low-pressure flash steam and secondary hot low-pressure flash oil in the second-stage hot low-pressure flash evaporation process; the operating pressure of the second-stage hot low-pressure flash evaporation process is greater than atmospheric pressure;

Secondary hot low-pressure flash oil, used as logistics MCP;

⑥The vapor-liquid miscible material formed by the hot high-fractionated oil S10-L after decompression is separated into hot low-pressure flash steam and hot low-pressure flash oil during the hot low-pressure flash evaporation process. The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

After decompression, the hot low-pressure flash oil enters the flash evaporation process of negative pressure operation. After the depressurization, the hot low-pressure flash oil enters the negative pressure operation state and the operating pressure is greater than the atmospheric pressure. It is used as logistics MCP.

In the present invention, generally, in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in the heavy oil R10F is greater than 50%;

⑴ In the reaction part R10 of heavy oil suspended bed hydrogenation conversion, in the presence of hydrogen, conventional liquid hydrocarbons, and the solid particle catalyst R10-CAT for heavy oil suspended bed hydrogenation conversion, there is or is not the presence of hydrogen-donating hydrocarbons, and the presence or absence of other solid particles. Under the condition of mixed phase materials, heavy oil R10F undergoes heavy oil suspended bed hydrogenation conversion reaction R10R including suspended bed hydrocracking reaction and is converted into reaction product R10P;

The solid particle catalyst R10-CAT contains at least Mo element, and the main working form of Mo in the reaction part R10 is M0S2;

Heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 70%, and meets at least one of the following conditions:

① Asphaltene weight concentration is greater than 12%;

②Kang’s carbon residue value is higher than 16%;

③The weight content of organic sulfur is higher than 0.5%;

④The weight content of organic nitrogen is higher than 0.15%;

⑤The organic metal weight content is higher than 0.015%;

In the reaction part R10, the single-pass weight conversion rate of hydrocracking of hydrocarbon components with conventional boiling points higher than 530°C in all feed oils is greater than 20%, so that at least 50% by weight of asphaltenes in the heavy oil R10F complete the hydrocracking reaction; All feed oils in the reaction section R10, including heavy oil R10F and circulating vacuum flash oil S50-FL-TOR10 from the vacuum flash bottom oil circulation section;

The heavy oil suspended bed hydroconversion reaction R10R includes a suspended bed hydrofinishing reaction, which enables at least 80% by weight of the organic metals in the heavy oil R10F to complete the hydrodemetallization reaction and completes the hydrogenation of at least 60% by weight of the organic sulfur in the heavy oil R10F. The desulfurization reaction is to complete the hydrodenitrification reaction of at least 30% by weight of organic nitrogen in the heavy oil R10F, so that the average Conian carbon residue value of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average Conian carbon residue value of the heavy oil R10F. 50%;

In the hot high-pressure separation part S10, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C based on the reaction product R10P is separated into hot high-fractionated gas S10-V and hot high-fractionated oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

An asphaltene-containing stream based on the quenched mixture stream MCP-BASE containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the base stream MCP-CS;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash distillation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in the external discharge vacuum flash evaporation base oil S50-FL-OUT is lower than 50% of the weight flow rate of hydrocarbon components with conventional boiling points higher than 530°C in heavy oil R10F. %;

⑸ In the vacuum flash evaporation bottom oil circulation part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash evaporation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is returned to the reaction part R10 as circulating vacuum flash oil S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating vacuum flash oil S50-FL-TOR10 or the circulating vacuum flash oil S50-FL-TOR10 is mixed and contacted with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F;

⑹ In the quenching oil supply part K100, the quenching oil KGS is selected from one or more of the following oils:

① In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280℃, and the temperature of the quenching oil KGS is higher than the temperature of the initial quenching oil KGS0 At least 40℃;

②In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270℃, and the temperature of the quenching oil KGS is higher than that of the initial quenching oil KGS0. The temperature is at least 40℃;

③ A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, the operating conditions are usually as follows: in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with conventional boiling points higher than 530°C in the heavy oil R10F is 75 to 98%;

⑴In the reaction part R10, the weight content of MOS2 in the liquid phase of the reaction process is 0.1~0.5%;

Heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 85%, and meets at least one of the following conditions:

① Asphaltene weight concentration is greater than 16%;

②Kang’s carbon residue value is higher than 24%;

③The weight content of organic sulfur is higher than 2.5%;

④The weight content of organic nitrogen is higher than 0.25%;

⑤The organic metal weight content is higher than 0.025%;

The operating conditions of reaction part R10 are: temperature 380~460℃, pressure 8.0~25.0MPa, hydrogen/raw oil volume ratio 50~4000, volume space velocity 0.1~10.0hr ^-1 ; weight chemical hydrogen of heavy oil R10F Consumption is 0.05~4.00%;

The operating conditions of the hot high-pressure separation part S10 are: the temperature is 360~460°C, the pressure is 8.0~25.0MPa, and hydrogen is injected or not injected into the liquid phase zone of the hot high-fraction oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

In the cooling stabilization part DT10, the logistics MCP with a temperature of T1 is mixed with the quenching oil KGS with a temperature of T3 to become a quenched mixed flow MCP-BASE with a temperature of T2. The cooling range of the logistics MCP is DT, DT=T1-T2, DT 25～75℃;

The ratio of the weight flow rate of quench oil KGS to the weight flow rate of logistics MCP is 0.01 to 0.65;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

The gas MCP-CS-FV composed of low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT based on the vacuum flash distillation bottom oil S50-FL is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The ratio of the weight flow rate of hydrocarbon components with a conventional boiling point higher than 530°C in the vented vacuum flash bottom oil S50-FL-OUT to the weight flow rate of hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F , less than 25%;

⑸ In the vacuum flash evaporation base oil circulation part, the ratio of the weight flow rate of the circulating vacuum flash oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 0.5 to 2.0.

In the present invention, the operating conditions are generally as follows: in the heavy oil suspended bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F is 88 to 95%;

⑴In the reaction part R10, the weight content of MOS ₂ in the liquid phase of the reaction process is 0.2 to 0.4%;

Heavy oil R10F has a conventional boiling point higher than 530°C and a weight concentration of hydrocarbon components greater than 90%, and meets at least one of the following conditions:

① Asphaltene weight concentration is greater than 20%;

②Kang’s carbon residue value is higher than 28%;

③The weight content of organic sulfur is higher than 3.5%;

④The weight content of organic nitrogen is higher than 0.45%;

⑤The organic metal weight content is higher than 0.050%;

The operating conditions of reaction part R10 are: temperature 400~440℃, pressure 10.0~17.0MPa, hydrogen/raw oil volume ratio 100~1500, volume space velocity 0.2~2.0hr ^-1 ; weight chemical hydrogen of heavy oil R10F Consumption is 2.00~3.50%;

The operating conditions of the hot high-pressure separation part S10 are: the temperature is 360~440°C, the pressure is 10.0~17.0MPa, and hydrogen is injected or not injected into the liquid phase zone of the hot high-percentage oil S10-L;

⑵ In the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the reaction product R10P, which contains hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C, is mixed with the quenching oil KGS to become a post-quenching mixture. LogisticsMCP-BASE;

In the cooling stabilization part DT10, the logistics MCP with a temperature of T1 is mixed with the quenching oil KGS with a temperature of T3 to become a quenched mixed flow MCP-BASE with a temperature of T2. The cooling range of the logistics MCP is DT, DT=T1-T2, DT is 35~65℃;

The ratio of the weight flow rate of quench oil KGS to the weight flow rate of logistics MCP is 0.01 to 0.65;

⑶Separation/fractionation part S50, including at least a vacuum flash evaporation step;

In the separation/fractionation part S50, the base stream MCP-CS flashes out the vapor MCP-CS-FV composed of the low-boiling point component LCOM to obtain asphaltene-containing solid particles containing hydrocarbon components with a conventional boiling point higher than 530°C. The vacuum flash evaporation base oil S50-FL of catalyst R10-CAT;

The gas MCP-CS-FV composed of low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

⑷ In the vacuum flash distillation bottom oil discharge part, at least part of the asphaltene-containing solid particle catalyst R10-CAT is based on the vacuum flash distillation bottom oil S50-FL and is mainly composed of hydrocarbon components with conventional boiling points higher than 530°C. The material is used as the outlet decompression flash evaporation base oil S50-FL-OUT;

The ratio of the weight flow rate of hydrocarbon components with a conventional boiling point higher than 530°C in the vented vacuum flash bottom oil S50-FL-OUT to the weight flow rate of hydrocarbon components with a conventional boiling point higher than 530°C in the heavy oil R10F , less than 12%;

⑸ In the vacuum flash evaporation base oil circulation part, the ratio of the weight flow rate of the circulating vacuum flash oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 1.0 to 2.0.

In the present invention, heavy oil R10F can be selected from one or more of the following streams:

①The bottom oil in the vacuum distillation process of crude oil;

②The base oil in the vacuum distillation process of shale oil;

③The base oil in the vacuum distillation process of oil sand oil;

④The base oil in the coal tar vacuum distillation process;

⑤Solvent deasphalted oil.

In the present invention, the quenching oil KGS can be one or more of the following oils:

① The condensate oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50;

② A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, usually, (3) in the separation/fractionation part S50, the hot high-fractionated oil S10-L is depressurized to obtain the miscible material S10-L-DP;

The miscible material S10-L-DP enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating conditions of the first hot low-pressure flash evaporation process are: the temperature is 340~440°C, The pressure is 0.35~2.0MPa; the first hot low fraction oil may or may not be in contact with the stripping water vapor;

After the pressure of the first hot low-separation oil is reduced, it enters the second hot low-pressure flash evaporation process and is separated into the second hot low-separation gas and the second hot low-separation oil; the operating conditions of the second hot low-pressure flash evaporation process are: the temperature is 330 ~ 430 ℃, pressure is 0.15~0.30MPa; the second thermal low-fractionated oil may or may not be in contact with the stripping water vapor; the operating pressure of the second thermal low-pressure flash evaporation process is lower than the operating pressure of the first thermal low-pressure flash evaporation process;

The second hot low-fractionated oil is depressurized and enters the first negative pressure flash evaporation process to be separated into the first negative pressure flash steam and the first negative pressure flash evaporation oil; the operating conditions of the first negative pressure flash evaporation process are: the temperature is 325 ~ 415℃, pressure is -0.55~-0.098MPa; the first negative pressure flash oil is in contact with or not in contact with the stripping water vapor; the operating pressure of the first negative pressure flash evaporation process is lower than that of the second hot low pressure flash evaporation process operating pressure;

The first negative pressure flash oil is used as the base oil of vacuum flash evaporation S50-FL;

The first hot low-component gas enters or does not enter the first hot low-component gas for separation in the distillation process;

The second hot low-component gas enters or does not enter the second hot low-component gas for separation in the distillation process;

The first thermal low-gas distillation process and the second thermal low-gas distillation process are set up separately or share a set of distillation processes;

The first negative pressure flash steam enters or does not enter the first negative pressure flash steam rectification process for separation;

The flash steam from the first hot low-pressure flash evaporation process is directly discharged from the first hot low-pressure flash evaporation process, or mixed with the liquid from the first hot low-pressure vapor distillation process and then discharged from the first hot low-pressure flash evaporation process.

The flash steam from the second hot low-pressure flash evaporation process is directly discharged from the second hot low-pressure flash evaporation process, or mixed with the liquid from the second hot low-pressure vapor distillation process and then discharged from the second hot low-pressure flash evaporation process.

The flash steam from the first negative pressure flash evaporation process is directly discharged from the first negative pressure flash evaporation process, or mixed with the liquid from the first negative pressure flash steam distillation process and then discharged from the first negative pressure flash evaporation process.

In the present invention, generally, (3) in the separation/fractionation part S50, the miscible material S10-L-DP is obtained after depressurizing the hot high-fractionated oil S10-L;

The miscible material S10-L-DP enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating conditions of the first hot low-pressure flash evaporation process are: the temperature is 340~440°C, The pressure is 0.35~2.0MPa; the first hot low fraction oil may or may not be in contact with the stripping water vapor;

After the pressure of the first hot low-separation oil is reduced, it enters the second hot low-pressure flash evaporation process and is separated into the second hot low-separation gas and the second hot low-separation oil; the operating conditions of the second hot low-pressure flash evaporation process are: the temperature is 330 ~ 430 ℃, pressure is 0.15~0.30MPa; the second thermal low-fractionated oil may or may not be in contact with the stripping water vapor; the operating pressure of the second thermal low-pressure flash evaporation process is lower than the operating pressure of the first thermal low-pressure flash evaporation process;

The second hot low-fractionated oil is depressurized and enters the first negative pressure flash evaporation process to be separated into the first negative pressure flash steam and the first negative pressure flash evaporation oil; the operating conditions of the first negative pressure flash evaporation process are: the temperature is 325 ~ 415℃, pressure is -0.55~-0.098MPa; the first negative pressure flash oil is in contact with or not in contact with the stripping water vapor; the operating pressure of the first negative pressure flash evaporation process is lower than that of the second hot low pressure flash evaporation process operating pressure;

After the first negative pressure flash oil is decompressed, it enters the second negative pressure flash evaporation process and is separated into the second negative pressure flash steam and the second negative pressure flash oil; the operating conditions of the second negative pressure flash evaporation process are: the temperature is 345 ~405℃, pressure is -0.090~-0.098MPa; in the second heat, the low fraction oil is in contact with or not in contact with the stripping water vapor; the operating pressure of the second negative pressure flash evaporation process is lower than that of the first negative pressure flash evaporation process operating pressure;

The second negative pressure flash oil is used as vacuum flash evaporation base oil S50-FL;

The first hot low-component gas enters or does not enter the first hot low-component gas for separation in the distillation process;

The second hot low-component gas enters or does not enter the second hot low-component gas for separation in the distillation process;

The first thermal low-gas distillation process and the second thermal low-gas distillation process are set up separately or share a set of distillation processes;

The first negative pressure flash steam enters or does not enter the first negative pressure flash steam rectification process for separation;

The second negative pressure flash steam enters or does not enter the second negative pressure flash steam rectification process for separation;

The first negative pressure flash steam distillation process and the second negative pressure flash steam distillation process are set separately or share a set of distillation processes;

The flash steam from the first hot low-pressure flash evaporation process is directly discharged from the first hot low-pressure flash evaporation process, or mixed with the liquid from the first hot low-pressure vapor distillation process and then discharged from the first hot low-pressure flash evaporation process.

The flash steam from the second hot low-pressure flash evaporation process is directly discharged from the second hot low-pressure flash evaporation process, or mixed with the liquid from the second hot low-pressure vapor distillation process and then discharged from the second hot low-pressure flash evaporation process.

The flash steam from the first negative pressure flash evaporation process is directly discharged from the first negative pressure flash evaporation process, or mixed with the liquid from the first negative pressure flash steam distillation process and then discharged from the first negative pressure flash evaporation process;

The flash steam from the second negative pressure flash evaporation process is directly discharged from the second negative pressure flash evaporation process, or mixed with the liquid from the second negative pressure flash steam distillation process and then discharged from the second negative pressure flash evaporation process.

In the present invention, generally, the distillation bottom oil discharged from the flash steam rectification process of the first hot low-pressure flash evaporation process and/or the distillation bottom oil discharged from the flash steam rectification process of the second hot low-pressure flash evaporation process enters The first hot low-pressure flash evaporation process and/or the second hot low-pressure flash evaporation process are in mixed contact with the flash steam of the first hot low-pressure flash evaporation process and/or the flash steam of the second hot low-pressure flash evaporation process, as a wash oil washing flash. Heavy components and solid particles in steam.

In the present invention, generally, the distillation bottom oil discharged from the flash steam distillation process of the first negative pressure flash evaporation process and/or the distillation bottom oil discharged from the flash steam distillation process of the second negative pressure flash evaporation process enters The first negative pressure flash evaporation process and/or the second negative pressure flash evaporation process are mixed and contacted with the flash steam of the first negative pressure flash evaporation process and/or the flash steam of the second negative pressure flash evaporation process, as a washing oil washing flash. Heavy components and solid particles in steam.

In the present invention, generally, the waxy oil component liquid stream discharged from the negative pressure distillation process of flash steam in the negative pressure flash evaporation process enters the first hot low pressure flash evaporation process and/or the second hot low pressure flash evaporation process, and is combined with the third hot low pressure flash evaporation process. The flash steam of the first hot low-pressure flash evaporation process and/or the flash steam of the second hot low-pressure flash evaporation process are mixed and contacted to wash the heavy components and solid particles in the flash steam of the washing oil.

In the present invention, generally, the waxy oil-containing liquid that does not contain vacuum residue is obtained by the distillation process of the flash steam of the first hot low-pressure flash evaporation process and/or the flash steam distillation process of the second hot low-pressure flash evaporation process. The phase hydrocarbon oil stream enters the negative pressure distillation process of the flash steam of the negative pressure flash evaporation process and is used as an intermediate feed.

In the present invention, usually, (3) in the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recovered;

In the separation recovery system S50-VD, based on the heat released by the condensation process of the gas MCP-CS-FV, the initial quench oil KGS0 from the quench oil supply part K100 is heated in the indirect heating step HX6030 to obtain the preheated initial quench oil KGS0- H, the flow based on the initial quenching oil KGS0-H after preheating is used as quenching oil KGS to enter the cooling stabilization part DT10;

The component composition of the quenching oil KGS is the same as or different from the component composition of the initial quenching oil KGS0. The weight flow rate of the quenching oil KGS is the same as or different from the weight flow rate of the initial quenching oil KGS0; the initial quenching oil KGS0 preheating changes to preheating The process of post-initial quenching oil KGS0-H, including or not including flash evaporation process, including or not including fractionation process;

⑹In the quenching oil supply part K100, provide initial quenching oil KGS0;

The initial quench oil KGS0 is the condensed oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50. It is preheated by the indirect heating step HX6030 in the separation/fractionation section S50 to obtain the quench oil KGS;

The initial quenching oil KGS0 is one or more of the following oils:

① In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280℃, and the temperature of the quenching oil KGS is higher than the temperature of the initial quenching oil KGS0 At least 40℃;

②In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270℃, and the temperature of the quenching oil KGS is higher than that of the initial quenching oil KGS0. The temperature is at least 40℃;

③ A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, usually, (3) in the separation/fractionation part S50, during normal operation, there is no oil heating furnace to provide heat, that is, no oil heating furnace is installed or the heating furnace through which the oil passes does not provide heat.

In the present invention, generally, (5) in the vacuum flash evaporation bottom oil circulation part, the ratio of the weight flow rate of the circulating vacuum flash evaporation oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 1.0 to 2.0.

The present invention, generally, (2) in the cooling and stabilizing part DT10, the asphaltene-containing stream MCP based on the thermal high-fractionated oil S10-L containing hydrocarbon components with a conventional boiling point higher than 530°C, and the quenching oil KGS based on the separation/fractionation part S50 After mixing, it becomes basic logistics MCP-CS;

⑶In the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

In the separation recovery system S50-VD, based on the heat released during the condensation process of the gas MCP-CS-FV, the initial quenching oil KGS0 is heated in the indirect heating step HX6030 to obtain the preheated initial quenching oil KGS0-H. Based on the initial quenching oil KGS0-H after preheating, The flow of quenching oil KGS0-H is used as quenching oil KGS to enter the cooling stabilization part DT10;

The component composition of the quenching oil KGS is the same as or different from the component composition of the initial quenching oil KGS0. The weight flow rate of the quenching oil KGS is the same as or different from the weight flow rate of the initial quenching oil KGS0; the initial quenching oil KGS0 preheating changes to preheating The process of post-initial quenching oil KGS0-H, including or not including the flash evaporation process KGSO-FPR, including or not including the fractionation process KGSO-DPR;

The flash steam of the flash evaporation process KGSO-FPR and/or the gas products of the fractionation process KGSO-DPR enter or do not enter the separation and recovery system S50-VD of the gas MCP-CS-FV;

⑹In the quenching oil supply part K100, provide initial quenching oil KGS0;

The initial quenching oil KGS0 is preheated by the indirect heating step HX6030 in the separation/fractionation section S50 to obtain the quenching oil KGS;

The initial quenching oil KGS0 is one or more of the following oils:

① In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280℃, and the temperature of the quenching oil KGS is higher than the temperature of the initial quenching oil KGS0 At least 40℃;

②In the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270℃, and the temperature of the quenching oil KGS is higher than that of the initial quenching oil KGS0. The temperature is at least 40℃;

③ A hydrocarbon stream containing waxy oil components based on cold high-fractionated oil, mainly composed of diesel components.

In the present invention, usually, (3) in the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recovered;

In the separation recovery system S50-VD, based on the heat released during the condensation process of the gas MCP-CS-FV, the initial quenching oil KGS0 is heated in the indirect heating step HX6030 to obtain the preheated initial quenching oil KGS0-H. Based on the initial quenching oil KGS0-H after preheating, The flow of quenching oil KGS0-H is used as quenching oil KGS to enter the cooling stabilization part DT10;

After the initial quenching oil KGS0 is converted into the preheated initial quenching oil KGS0-H, the indirect heating step HX6030 uses at least 2 series preheating processes. The initial quenching oil KGS0 undergoes a flash evaporation operation after the upstream preheating process to obtain the removal steam. The liquid enters the adjacent downstream preheating process, and finally the preheated initial quench oil KGS0-H discharged from the indirect heating step HX6030 is flash evaporated to remove the vapor KGS0-H-V and the liquid is used as quench oil KGS.

In the present invention, generally, in the indirect heating step HX6030, the gas KGSO-H-V enters the fractionation tower of the separation and recovery system S50-VD of the gas MCP-CS-FV.

In the present invention, usually, (3) in the separation/fractionation part S50, the initial quenching oil KGS0 comes from the positive pressure fractionation process and is mainly composed of diesel components. The temperature of the initial quenching oil KGS0 is 180~280°C, and the temperature of the quenching oil KGS is higher than the initial The temperature of the quenching oil KGS0 is at least 40°C.

In the present invention, usually, (3) in the separation/fractionation part S50, the initial quenching oil KGS0 comes from the negative pressure fractionation process and is mainly composed of wax oil components. The temperature of the initial quenching oil KGS0 is 130~270°C, and the temperature of the quenching oil KGS is higher than The initial temperature of the quench oil KGS0 is at least 40°C.

In the present invention, (1) hydrogen-donating hydrocarbons can be used in the reaction part R10 of the heavy oil suspended bed hydrogenation conversion.

In the present invention, generally, (2) in the cooling stabilization section DT10, the asphaltene-containing stream MCP based on the thermal high-fractionation oil S10-L containing hydrocarbon components with a conventional boiling point higher than 530°C is combined with the quenching oil KGS from the separation/fractionation section S50 After mixing, it becomes basic logistics MCP-CS;

⑶In the separation/fractionation part S50, the vapor MCP-CS-FV composed of the low boiling point component LCOM enters the separation and recovery system S50-VD and is separated and recycled;

In the separation recovery system S50-VD, based on the heat released during the condensation process of the gas MCP-CS-FV, the initial quenching oil KGS0 is heated in the indirect heating step HX6030 to obtain the preheated initial quenching oil KGS0-H. Based on the initial quenching oil KGS0-H after preheating, The flow of quenching oil KGS0-H is used as quenching oil KGS to enter the cooling stabilization part DT10;

⑹ In the quench oil supply section K100, the initial quench oil KGS0 is the condensed oil BASE-KGS0 obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50. The distillate oil BASE-KGS0 is first boosted and then heated. The materials are used as quenching oil KGS.

In the present invention, usually, in the (3) separation/fractionation part S50, the temperature of the initial quenching oil KGS0 is 110~200°C, and the temperature of the quenching oil KGS is 230~300°C.

In the present invention, generally, in the (3) separation/fractionation part S50, the temperature of the initial quenching oil KGS0 is 130~180°C, and the temperature of the quenching oil KGS is 260~290°C.

In the present invention, usually (2) in the cooling stable part DT10, the ratio of the weight flow rate of the quenching oil KGS to the weight flow rate of the logistics MCP is 0.01 to 0.15 or 0.15 to 0.30 or 0.30 to 0.45 or 0.45 or more.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is circulating oil;

Quench oil KGS is the condensed oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50;

Basic logistics MCP-CS is selected from one or more of the following logistics:

① The mixed-phase stream formed by depressurizing the hot high-fragment oil S10-L is used as the logistics MCP, and is mixed with the quenching oil KGS to become the basic logistics MCP-CS;

② The mixed-phase stream formed by depressurizing the hot high-separation oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separation gas, the first hot low-separation oil, and the first hot low-separation oil is used as the logistics MCP; the first The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

③The mixed-phase stream formed by depressurizing the hot high-fractionated oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fractionated gas and the first hot low-fractionated oil. The first hot low-fractionated oil is used as the logistics MCP; the first The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

After the first hot low-separation oil is depressurized, it enters the second hot low-pressure flash evaporation process and is separated into the second hot low-separation gas and the second hot low-separation oil. The second hot low-separation oil is used as the logistics MCP; the second hot low-pressure flash evaporation process The operating pressure is greater than atmospheric pressure; the operating pressure of the second hot low-pressure flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

④The mixed-phase stream formed by depressurizing the hot high-fractionated oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fractionated gas and the first hot low-fractionated oil. The first hot low-fractionated oil is used as the logistics MCP; the first The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low-content oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process, and the first negative pressure flash oil is used as the logistics MCP;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

In the second negative pressure flash evaporation process, the base stream MCP-CS is separated into the second negative pressure flash steam and the second negative pressure flash oil; the operating pressure of the second negative pressure flash evaporation process is lower than that of the first negative pressure flash evaporation process. operating pressure;

Separate the condensed oil obtained from the second negative pressure flash steam as quench oil KGS.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is circulating oil;

In the quenching oil supply part K100, the mixed-phase stream formed by depressurizing the hot high-fractionated oil S10-L is used as logistics MCP, and after being mixed with the quenching oil KGS, it becomes the basic logistics MCP-CS;

Quench oil KGS is the condensed oil obtained by separating the flash gas of the basic stream MCP-CS in the separation/fractionation section S50;

Quench oil KGS, selected from one or more of the following logistics:

① The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil;

The condensed oil obtained by separating the first hot low-fractionated gas in the separation/fractionation part S50 is used as quenching oil KGS;

② The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low-fragmented gas enters the separation and/or fractionation process of the first hot low-dividing gas for joint recovery;

The condensed oil obtained by separating the first hot low-fractionated gas in the separation/fractionation part S50 is used as quenching oil KGS;

③The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low fraction oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process;

In the separation/fractionation part S50, the condensed oil obtained from the first negative pressure flash steam is separated as quench oil KGS;

④The basic logistics MCP-CS enters the first hot low-pressure flash evaporation process and is separated into the first hot low-separated gas and the first hot low-separated oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-pressure oil is depressurized and enters the second hot low-pressure flash evaporation process and is separated into a second hot low-separation gas and a second hot low-separation oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure of the flash evaporation process is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low fraction oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process;

The first negative pressure flash oil is separated into a second negative pressure flash steam and a second negative pressure flash oil during the second negative pressure flash evaporation process; the operating pressure of the second negative pressure flash evaporation process is lower than that of the first negative pressure flash evaporation process. operating pressure of the process;

The second negative pressure flash steam enters the separation and/or fractionation process of the first negative pressure flash steam for joint recovery;

The condensed oil obtained from the first negative pressure flash steam is separated in the separation/fractionation part S50 as quench oil KGS.

In the present invention, generally, (6) in the quenching oil supply part K100, the depressurized stream of the hot high-fractionated oil S10-L enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fractionated gas and the first hot low-fractionated oil; The operating pressure of the first hot low-pressure flash evaporation process is greater than the atmospheric pressure; the first hot low-percentage oil is used as the logistics MCP;

Logistics MCP and quench oil KGS are mixed to become basic logistics MCP-CS;

A portion of the base oil-cooled stream obtained from the flash evaporation process based on the base stream MCP-CS is used as quenching oil KGS, which is selected from one or more of the following streams:

① The basic logistics MCP-CS enters the second hot low-pressure flash evaporation process and is separated into the second hot low-pressure flash evaporation process and the second hot low-separated oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low-fragmented gas enters the separation and/or fractionation process of the first hot low-dividing gas for joint recovery;

The condensed oil obtained by separating the first hot low-fractionated gas in the separation/fractionation part S50 is used as quenching oil KGS;

② The basic logistics MCP-CS enters the second hot low-pressure flash process and is separated into the second hot low-separated gas and the second hot low-separated oil; the operating pressure of the second hot low-pressure flash evaporation process is greater than atmospheric pressure; the second hot low-pressure flash evaporation process The operating pressure is lower than the operating pressure of the first hot low-pressure flash evaporation process;

The second hot low fraction oil is separated into the first negative pressure flash steam and the first negative pressure flash oil during the first negative pressure flash evaporation process;

The first negative pressure flash steam enters the separation and/or fractionation process of the first negative pressure flash steam for recovery;

The condensed oil obtained from the first negative pressure flash steam is separated in the separation/fractionation section S50 as quench oil KGS.

In the present invention, generally, (2) in the cooling and stabilizing part DT10, the asphaltene-containing stream MCP00 based on the reaction product R10P containing hydrocarbon components with a conventional boiling point lower than 530°C and a hydrocarbon component with a conventional boiling point higher than 530°C is split into a 2-way stream. MCP01, MCP02, logistics MCP01 is used as the first characteristic logistics to obtain the circulating vacuum flash evaporation oil S50-FL-TOR10, and logistics MCP02 is used as the second characteristic logistics to obtain the external exhaust vacuum flash evaporation base oil S50-FL-OUT. logistics;

The first characteristic stream MCP01 is mixed with the first quench oil KGS01 to become the first post-quench mixed stream MCP01-BASE;

Based on the first quenched mixture stream MCP01-BASE, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the first base stream MCP01-CS;

The second characteristic stream MCP02 is mixed with the second quench oil KGS02 to become the second quenched mixed stream MCP02-BASE;

Based on the second quenched mixture stream MCP02-BASE, the asphaltene-containing stream containing hydrocarbon components with a conventional boiling point higher than 530°C is used as the second base stream MCP02-CS;

⑶In the separation/fractionation part S50, after the first base stream MCP01-CS flashes out the first vapor MCP01-CS-FV composed of the low-boiling point component MCP01-LCOM, hydrocarbons containing conventional boiling points higher than 530°C are obtained. The first-pass decompression flash evaporation bottom oil MCP01-S50-FL of the asphaltene-containing solid particle catalyst R10-CAT is a component;

In the separation/fractionation part S50, after the second path basic stream MCP02-CS flashes out the second path vapor MCP02-CS-FV composed of the low-boiling point component MCP02-LCOM, a hydrocarbon group containing a conventional boiling point higher than 530°C is obtained. Second-pass vacuum flash evaporation bottom oil MCP02-S50-FL containing asphaltene-containing solid particle catalyst R10-CAT;

⑷ In the part where the vacuum flash distillation bottom oil is discharged, part or all of the second vacuum flash distillation bottom oil MCP02-S50-FL is used as the discharge vacuum flash distillation bottom oil S50-FL-OUT;

⑸ In the vacuum flash evaporation base oil circulation part, part or all of the first vacuum flash evaporation base oil MCP01-S50-FL is used as circulating vacuum flash evaporation oil MCP01-S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating vacuum flash oil MCP01-S50-FL-TOR10 or the circulating vacuum flash oil MCP01-S50-FL-TOR10 is mixed with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F. touch;

With or without the presence or absence of part of the second decompression flash evaporation base oil MCP02-S50-FL, return to the reaction part R10 to be used as circulating oil MCP02-S50-FL-TOR10;

In the reaction part R10, the intermediate hydrogenation product of the circulating oil MCP02-S50-FL-TOR10 or the circulating oil MCP02-S50-FL-TOR10 is mixed and contacted with the intermediate hydrogenation product of the heavy oil R10F or the heavy oil R10F;

⑹ In the quenching oil supply part K100, the first quenching oil KGS01 is selected from one or more of the following logistics:

In the quench oil supply section K100, the first quench oil KGS01 is the condensed oil obtained by separating the flash gas of the first basic stream MCP01-CS in the separation/fractionation section S50;

In the quench oil supply section K100, the second quench oil KGS02 is the condensed oil obtained by separating the flash gas of the second basic stream MCP02-CS in the separation/fractionation section S50.

In the present invention, generally, (6) in the quenching oil supply part K100, the first quenching oil KGS01 is the condensed oil obtained in the separation/fractionation part S50 based on the first basic stream MCP01-CS flash gas, and is selected from one of the following streams One or more species:

① Mainly composed of heavy diesel components and containing waxy oil components, coming from the positive pressure fractionation process based on the first basic stream MCP01-CS flash gas;

② Mainly composed of wax oil components with conventional boiling points lower than 430°C, derived from the negative pressure fractionation process based on the first basic stream MCP01-CS flash gas;

In the quenching oil supply section K100, the second quenching oil KGS02 is the condensed oil obtained in the separation/fractionation section S50 based on the second basic stream MCP02-CS flash gas, and is selected from one or more of the following streams:

① Mainly composed of heavy diesel components and containing waxy oil components, coming from the positive pressure fractionation process based on the second basic stream MCP02-CS flash gas;

② Mainly composed of wax oil components with a conventional boiling point lower than 430°C, derived from the negative pressure fractionation process based on the second basic stream MCP02-CS flash gas.

In the present invention, generally, (3) in the separation/fractionation part S50, the second path basic stream MCP02-CS flashes out the low boiling point component MCP02-LCOM and the second path vapor MCP02-CS-FV separation and recovery system MCP02-CS -FV-SYS, separate and recovery system MCP01-CS-FV-SYS for the first vapor MCP01-CS-FV consisting of the first basic stream MCP01-CS that flashes out the low-boiling component MCP01-LCOM, respectively. Set up or jointly set up to share at least part of the system.

In the present invention, usually, (3) in the separation/fractionation part S50, the first characteristic stream MCP01 enters the first hot low-pressure flash evaporation process and is separated into the first hot low-fraction gas and the first hot low-fraction gas. Oil; the operating pressure of the first hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-separation oil in the first path is depressurized and then enters the second hot low-pressure flash evaporation process in the first path and is separated into the second hot low-separation gas in the first path, the second hot low-separation oil in the first path; the second hot low-separation oil in the first path; The operating pressure of the thermal low-pressure flash evaporation process is greater than the atmospheric pressure; the operating pressure of the first and second thermal low-pressure flash evaporation processes is lower than the operating pressure of the first and first thermal low-pressure flash evaporation processes;

The first second hot low fraction oil is separated into the first first negative pressure flash steam and the first negative pressure flash oil in the first negative pressure flash evaporation process;

In the separation/fractionation part S50, the second characteristic stream MCP02 enters the first hot low-pressure flash evaporation process of the second path and is separated into the first hot low-fragmented gas of the second path and the first hot low-fragmented oil of the second path; 1. The operating pressure of the hot low-pressure flash evaporation process is greater than atmospheric pressure;

The first hot low-fractionated oil in the second path is depressurized and enters the second hot low-pressure flash evaporation process in the second path and is separated into the second hot low-percentage gas in the second path, the second hot low-percentage oil in the second path; the second hot low-percentage oil in the second path; The operating pressure of the hot low-pressure flash evaporation process is greater than the atmospheric pressure; the operating pressure of the second hot low-pressure flash evaporation process of the second path is lower than the operating pressure of the first hot low-pressure flash evaporation process of the second path;

The second hot low-carbon oil in the second path is separated into the first negative pressure flash steam in the second path and the first negative pressure flash oil in the second path during the first negative pressure flash evaporation process in the second path;

The first hot low-fractionated gas from the second path and the first hot low-fragmented gas from the first path are mixed and separated in the first hot low-fractionated gas separation and recovery system;

The second hot low-fractionated gas from the second path and the second hot low-fragmented gas from the first path are mixed and separated in the second hot low-fractionated gas separation and recovery system;

The first negative pressure flash steam from the first channel and the first negative pressure flash steam from the second channel are mixed and separated in the first negative pressure flash steam separation and recovery system.

In the present invention, usually, the second first hot low-pressure flash evaporation process and the first first hot low-pressure flash evaporation process are carried out in different spaces separated by partition plates in the pressure-bearing shell of the same container. The vapor phase space of the first hot low-pressure flash evaporation process is connected with the vapor phase space of the first hot low-pressure flash evaporation process;

The second hot low-pressure flash evaporation process of the second pass and the second hot low-pressure flash evaporation process of the first pass are carried out in different spaces separated by partition plates in the pressure-bearing shell of the same vessel. The second hot low-pressure flash evaporation process of the second pass The vapor phase space of the process is connected with the vapor phase space of the first and second hot low-pressure flash evaporation process;

The second first negative pressure flash evaporation process and the first first negative pressure flash evaporation process are carried out in different spaces separated by partition plates in the shell of the same container that bears negative pressure. The second first negative pressure flash evaporation process is The vapor phase space of the flash evaporation process is connected with the vapor phase space of the first negative pressure flash evaporation process.

In the present invention, usually, (3) in the separation/fractionation part S50, in the positive pressure separation process, the base stream MCP-CS is separated into hot low-fractionated gas and hot low-fragmented oil;

The condensed oil obtained by separating the first hot low-component gas is used as quenching oil KGS;

The way to separate the first hot low-component gas is to use the rectification section T11. The first hot low-component gas enters the lower part of the rectification section T11 and flows from bottom to upward along the rectification section T11 to fractionate the product: the bottom oil of the rectification section T11. , at least part of it is used as the logistics of quenching oil KGS, 1 or 2 or more lines of gas oil, and tower top exhaust gas;

Distillation section T11 uses oil-cooled reflux extracted from the middle section and/or cold circulation cold reflux at the top of the tower and/or cold reflux at the top of the tower to create a mass transfer liquid phase;

The hydrocarbon stream with or without a waxy oil component based on cold high-fractionated oil, which mainly consists of diesel components, enters the distillation section T11 for joint recovery.

In the present invention, generally, a hydrocarbon stream with or without a waxy oil component based mainly on a diesel component based on cold high-fractionated oil enters the distillation section T11 above the extraction port of the distillate used as quench oil KGS , the location of the tower section below the gas oil extraction outlet.

In the present invention, generally, the gas oil enters the gas diesel light component removal tower and is separated into the bottom diesel oil of the gas diesel light component removal tower and the top gas of the gas diesel light component removal tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T11.

In the present invention, two or more channels of gas oil from the distillation section T11 can enter the same gas diesel light component removal tower and be separated into the bottom diesel oil of the gas diesel light component removal tower and the gas oil light component removal tower air at the top of the tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T11.

In the present invention, usually, the operating pressure of the reflux tank of the gas oil light component removal tower is 0.105-0.5MPa (absolute pressure).

In the present invention, usually, (3) in the separation/fractionation part S50, in the positive pressure separation process, the base stream MCP-CS is separated into hot low-fractionated gas and hot low-fractionated oil; in the negative pressure separation process, the hot low-fractionated oil is separated into Negative pressure flash steam, negative pressure flash evaporation base oil;

The condensed oil obtained by separating the negative pressure flash steam is used as quench oil KGS;

The way to separate the negative pressure flash steam is to use the negative pressure rectification section T22. The negative pressure flash steam enters the lower part of the negative pressure rectification section T22 and flows from bottom to upward along the rectification section T22 to fractionate the product: bottom oil in the rectification section T22. , at least part of it is used as the logistics of quenching oil KGS and the exhaust gas at the top of the tower;

The distillation section T22 uses the oil-cooled reflux extracted from the middle section and/or the cold circulation cold reflux at the top of the tower and/or the cold reflux at the top of the tower to create the mass transfer liquid phase;

The hydrocarbon stream with or without a waxy oil component based on cold high-fractionated oil, which mainly consists of diesel components, enters the distillation section T22 for joint recovery.

In the present invention, generally, a hydrocarbon stream with or without a waxy oil component based on cold high-fractionated oil, mainly composed of diesel components, enters the distillation section T22 above the extraction port of the distillate used as quench oil KGS , the location of the tower section below the gas oil extraction outlet.

In the present invention, generally, the gas oil enters the gas diesel light component removal tower and is separated into the bottom diesel oil of the gas diesel light component removal tower and the top gas of the gas diesel light component removal tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T22.

In the present invention, two or more channels of gas oil from the rectification section T22 can enter the same gas diesel light component removal tower and be separated into the bottom diesel oil of the gas diesel light component removal tower and the gas oil light component removal tower air at the top of the tower;

The overhead gas from the light component tower is removed from the gas oil and returned to a position above the gas oil extraction port inside the distillation section T22.

In the present invention, usually, the operating pressure of the reflux tank of the gas oil light component removal tower is 0.105-0.5MPa (absolute pressure).

In the present invention, generally, the use of T22 base oil in the rectification section is selected from one or more of the following:

① Return to the R10 cycle reaction of the reaction part of heavy oil suspended bed hydrogenation conversion;

② Inside the distillation section T22, it directly enters the negative pressure flash evaporation bottom oil without passing through the oil collection tank;

③After mixing with a part of the negative pressure flash evaporation base oil, return to the reaction part R10 of the heavy oil suspension bed hydrogenation conversion for cycle reaction.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is a hydrocarbon oil rich in aromatics, and more than 80% of the quenching oil KGS is vaporized in the separation/fractionation part S50 and enters the flash gas of the basic stream MCP-CS , thereby bringing the heat absorbed in the cooling stabilization part DT10 into the flash gas of the basic stream MCP-CS for utilization. During the condensation process of the flash gas of the basic stream MCP-CS, the gas phase components from the quenching oil KGS More than 80% complete the condensation process to release heat.

In the present invention, generally, (6) in the quenching oil supply part K100, the quenching oil KGS is a hydrocarbon oil rich in aromatics, and more than 95% of the quenching oil KGS is vaporized in the separation/fractionation part S50 and enters the flash steam of the basic stream MCP-CS In the body, the heat absorbed in the cooling stabilization part DT10 is brought into the flash gas of the basic stream MCP-CS and utilized. During the condensation process of the flash gas of the basic stream MCP-CS, the gas phase group from the quenching oil KGS More than 95% of the condensation process is completed to release heat.

The following describes the general control principles of the gas phase hydrogen sulfide concentration in the hydrogenation reaction process of the present invention.

For the suspended bed hydrocracking process of heavy oil with high nitrogen content and low sulfur content, in order to maintain the lowest hydrogen sulfide partial pressure in the initial reaction process, any kind of supplementary sulfur can be added to any hydrogenation reaction process as needed, but It is usually added to the upstream hydrogenation reaction process inlet to ensure the minimum hydrogen sulfide concentration necessary for the reaction process, such as 500ppm (v) or 1000ppm (v) or 3000ppm (v) and other expected specified values to ensure the necessary hydrogen sulfide for the catalyst. The partial pressure shall not be lower than the minimum specified value to ensure the necessary sulfurization state of the catalyst. The supplementary sulfur can be materials containing hydrogen sulfide or that can be converted into hydrogen sulfide without adverse effects on the hydrogenation conversion process, such as gas or oil containing hydrogen sulfide, or liquid sulfur that generates hydrogen sulfide after contact with high-temperature hydrogen. Or carbon disulfide or dimethyl disulfide, etc.

The general principles of the high-pressure separation process of the hydrogenation reaction effluent of the present invention are described in detail below.

The high-pressure separation process of hydrogenation reaction effluent usually includes a cold high-pressure separator. When the hydrocarbon oil in the hydrogenation reaction effluent has a high density (for example, a density close to water) or a high viscosity, or is emulsified with water and is difficult to separate, or contains solid particles, It is necessary to set up a hot high-pressure separator with an operating temperature of usually 150 to 450°C. At this time, the hydrogenation reaction effluent enters the hot high-pressure separator and is separated into a hot high-pressure gas that is mainly composed of hydrogen in volume and a gas that is mainly composed of conventional liquid. Hot high-fractionated oil liquid composed of hydrocarbons and possible solids. The hot high-fractionated gas enters the cold high-pressure separator with an operating temperature of usually 20 to 80°C and is separated into cold high-fractionated oil and cold high-fractionated gas. Due to a large number of high-boiling point components Entering the hot high-fractionated oil liquid, the following goals are achieved: the cold high-fractionated oil becomes less dense or viscous or is easily separated from water. The high-pressure separation process of the hydrogenation reaction effluent also has the advantage of reducing heat loss by setting up a hot high-pressure separator, because the hot high-separation oil liquid can avoid the cooling process of using an air cooler or water cooler that the hot high-separation gas undergoes. At the same time, part of the hot high-fractionation oil liquid can be returned to the upstream hydrogenation reaction process for recycling to improve the overall raw material properties of the hydrogenation reaction process that receives the circulating oil, or the circulating hot high-fractionation oil can be cyclically hydrogenated.

Between the hot high-pressure separation part and the cold high-pressure separation part, a warm-high-pressure separation part can be set up as needed. At this time, the hot high-pressure gas is cooled and becomes a gas-liquid two-phase material, which is separated into a gas-liquid two-phase material in the warm-high pressure separator. A high-temperature and high-temperature gas separation gas mainly composed of hydrogen and a high-temperature and high-temperature separation oil liquid mainly composed of conventional liquid hydrocarbons and possible solids. The high-temperature and high-temperature gas separation gas enters the cold high-pressure separation part for cooling and gas-liquid separation.

Before the hydrogenation reaction effluent or hot high-temperature gas or high-temperature gas enters the cold high-pressure separation part, the temperature is usually lowered (usually by exchanging heat with the reaction part feed) to about 220 to 100°C (the temperature should be higher than The crystallization temperature of ammonium hydrogen sulfide and the crystallization temperature of ammonium chloride in the gas phase of the hydrogenation reaction effluent), and then wash water is usually injected into it to form the hydrogenation reaction effluent after water injection. It may be necessary to set up two or more water injection points. Water is used to absorb ammonia and other impurities that may be produced, such as hydrogen chloride, etc., and the aqueous solution after absorbing ammonia must absorb hydrogen sulfide. In the cold high-pressure separation part, the hydrogenation reaction effluent after water injection is separated into: a cold high-fractionated gas mainly composed of hydrogen in volume, a cold high-fractionated oil mainly composed of conventional liquid hydrocarbons and dissolved hydrogen, and a mainly cold high-fractionated oil. Cold, high-density water composed of water with ammonia and hydrogen sulfide dissolved in it. The ammonia content of the cold high-density water is generally 0.5-15% (w), preferably 1-8% (w). One purpose of injecting wash water is to absorb ammonia and hydrogen sulfide in the hydrogenation reaction effluent to prevent the formation of hydrogen sulfide or ammonium polysulfide crystals that block the heat exchanger channels and increase the system pressure drop. The injection amount of the wash water should be determined according to the following principles: on the one hand, the wash water is divided into vapor phase water and liquid phase water after being injected into the hydrogenation reaction effluent. The amount of liquid phase water must be greater than zero, preferably the total wash water. 30% or more of the amount; on the other hand, the wash water is used to absorb ammonia in the hydrogenation reaction effluent to prevent the ammonia concentration in the high-fragmented gas from being too high and reducing the catalyst activity. Usually, the lower the ammonia volume concentration in the high-divided gas The better, generally no more than 200ppm(v), preferably no more than 50ppm(v). The operating pressure of the cold high-pressure separator is the pressure of the hydrogenation reaction part minus the actual pressure drop. The difference between the operating pressure of the cold high-pressure separation part and the hydrogenation reaction pressure should not be too low or too high, generally 0.35~3.2MPa, Usually 0.5~1.5MPa. The hydrogen volume concentration value of the cold high-temperature gas should not be too low (leading to an increase in the operating pressure of the device). Generally, it should be no less than 70% (v), preferably no less than 80% (v), and preferably no less than 85%(v). As mentioned above, at least a part, usually 85 to 100%, of the cold high-temperature gas is returned and recycled in the hydrogenation reaction part to provide the necessary hydrogen amount and hydrogen concentration in the hydrogenation reaction part; in order to improve the investment efficiency of the device, circulation must be ensured The hydrogen concentration is not lower than the aforementioned lower limit. Therefore, according to the specific raw material properties, reaction conditions, and product distribution, a part of the cold high-fractionated gas can be eliminated to eliminate the methane and ethane produced by the reaction. For the discharged cold high-fractionated gas, conventional membrane separation process or pressure swing adsorption process or oil washing process can be used to separate hydrogen and non-hydrogen gas components, and the recovered hydrogen can be used as new hydrogen.

For the heavy oil suspended bed hydrocracking process, because of the huge yields of CH4, C2H6, and H2S, usually part or all of the cold high-fractionated gas, such as about 30 to 100% cold high-fractionated gas, is purified through a membrane separation process and the resulting permeated hydrogen is added. After being pressured, it is returned to the hydrogenation reaction process. The non-permeated gas can be subjected to hydrogenation by PSA or "hydrogen production by steam conversion + hydrogenation by PSA" and then pressurized and returned to the hydrogenation reaction process for recycling.

New hydrogen enters the hydrogenation part to supplement the hydrogen consumed during the hydrogenation reaction. The higher the concentration of new hydrogen, the better. Generally, it should not be less than 95% (v), and preferably not less than 99% (v). All new hydrogen can be introduced into any hydrogenation reaction section, preferably into the first hydrogenation reactor.

In the present invention, in any reaction process, the hydrogen stream used can be all new hydrogen, all recycled hydrogen, or a mixed gas of new hydrogen and recycled hydrogen.

Claims (47)

1. The cooling separation method of the tail oil circulation type heavy oil suspension bed hydrocracking product high-temperature oil is characterized by comprising the following steps of:

a heavy oil suspension bed hydroconversion process U100 for converting heavy oil into low molecular weight hydrocarbons, comprising a reaction section R10 for performing heavy oil suspension bed hydroconversion, a quench stabilization section DT10 for injecting quench oil KGS comprising an asphaltene-containing stream MCP having a conventional boiling point below 530 ℃ and a conventional boiling point above 530 ℃ hydrocarbon component based on reaction product R10P, a separation/fractionation section S50 for a base stream MCP-CS, a reduced pressure flash bottoms offtake section, a reduced pressure flash bottoms recycle section, a quench oil supply section K100;

In the heavy oil suspension bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with the conventional boiling point higher than 530 ℃ in the heavy oil R10F is higher than 30%;

the method comprises the steps that in a reaction part R10 of heavy oil suspension bed hydroconversion, heavy oil R10F and circulating vacuum flash oil S50-FL-TOR10 from a vacuum flash bottom oil circulation part are subjected to heavy oil suspension bed hydroconversion reaction R10R comprising suspension bed hydrocracking reaction to obtain reaction product R10P under the condition that hydrogen, conventional liquid hydrocarbon and solid particle catalyst R10-CAT for heavy oil suspension bed hydroconversion are simultaneously present or absent hydrogen-supplying hydrocarbon and mixed phase materials of other solid particles are present or absent;

the solid particle catalyst R10-CAT at least comprises Mo element, and the main working form of Mo in the reaction part R10 is M0S2;

heavy oil R10F, the weight concentration of hydrocarbon components with the conventional boiling point higher than 530 ℃ is higher than 50%, and the heavy oil contains one or more of asphaltene, organic sulfur, organic nitrogen and organic metal impurity components;

heavy oil R10F is taken as fresh reaction feed of a reaction part R10 and is a mixed raw material formed by mixing single-property raw material oil or branched raw materials with different properties;

when the heavy oil R10F is formed by mixing several branched raw oils with different properties, at least one branched raw oil contains asphaltene, and one or more other branched raw oils contain or do not contain asphaltene;

The heavy oil suspension bed hydro-conversion reaction R10R comprises a suspension bed hydro-cracking reaction, so that at least one part of hydrocarbon components with the conventional boiling point higher than 530 ℃ in the heavy oil R10F are subjected to the hydro-cracking reaction and converted into hydrocarbon products with smaller molecular weight;

the heavy oil suspension bed hydro-conversion reaction R10R comprises a suspension bed hydrofining reaction, so that at least part of impurity elements in the heavy oil R10F complete the hydro-impurity removal reaction, and at least part of unsaturated carbon-carbon bonds of at least part of hydrocarbon components in the heavy oil R10F are hydrogenated and saturated; the hydrodeimpurity reaction comprises one or more of hydrodemetallization reaction, hydrodesulfurization reaction, hydrodenitrogenation reaction and hydrodeoxygenation reaction;

the average asphaltene weight concentration of all conventional liquid hydrocarbons in the reaction product R10P is lower than the average asphaltene weight concentration of heavy oil R10F;

the average Conn carbon residue value of all conventional liquid hydrocarbons in the reaction product R10P is lower than that of heavy oil R10F;

the average organic sulfur weight content of all conventional liquid hydrocarbon in the reaction product R10P is lower than that of heavy oil R10F;

the average organic nitrogen weight content of all conventional liquid hydrocarbons in the reaction product R10P is lower than that of heavy oil R10F;

The average organic metal weight content of all conventional liquid hydrocarbon in the reaction product R10P is lower than that of heavy oil R10F;

in the hot high pressure separation section S10, an asphaltene-containing stream comprising hydrocarbon components having a conventional boiling point above 530 ℃ based on the reaction product R10P is separated into a hot high-pressure gas S10-V and a hot high-pressure oil S10-L;

in the cooling stabilizing section DT10, an asphaltene-containing material flow MCP containing hydrocarbon components with a conventional boiling point lower than 530 ℃ and hydrocarbon components with a conventional boiling point higher than 530 ℃ based on a reaction product R10P is mixed with quenching oil KGS to form a quenched mixture material flow MCP-BASE;

an asphaltene-containing stream comprising hydrocarbon components having conventional boiling points above 530 ℃ based on the quenched mixture stream MCP-BASE as a BASE stream MCP-CS;

a third separation/fractionation section S50 comprising at least a reduced pressure flash step;

in the separation/fractionation section S50, the base stream MCP-CS flashes off the vapor MCP-CS-FV composed of the low boiling components LCOM to obtain a reduced pressure flash bottoms S50-FL containing asphaltene-containing solid particulate catalyst R10-CAT containing hydrocarbon components having a conventional boiling point above 530 ℃;

at least one part of the material containing asphaltene and containing solid particle catalyst R10-CAT, which is based on hydrocarbon components with the conventional boiling point higher than 530 ℃ and mainly comprises the pressure-reduced flash evaporation bottom oil S50-FL, is used as the pressure-reduced flash evaporation bottom oil S50-FL-OUT;

The weight flow rate of the hydrocarbon component with the conventional boiling point higher than 530 ℃ in the discharged reduced pressure flash bottom oil S50-FL-OUT is 70% lower than the weight flow rate of the hydrocarbon component with the conventional boiling point higher than 530 ℃ in the heavy oil R10F;

fifthly, in a reduced pressure flash evaporation bottom oil circulation part, at least one part of materials containing solid particle catalyst R10-CAT which mainly consists of hydrocarbon components with the conventional boiling point higher than 530 ℃ based on reduced pressure flash evaporation bottom oil S50-FL is returned to the reaction part R10 as circulating reduced pressure flash evaporation oil S50-FL-TOR 10;

in the reaction part R10, the circulating vacuum flash oil S50-FL-TOR10 or the intermediate hydrogenation product of the circulating vacuum flash oil S50-FL-TOR10 is mixed and contacted with heavy oil R10F or the intermediate hydrogenation product of heavy oil R10F;

in the quenching oil supply section K100, the quenching oil KGS is hydrocarbon oil rich in aromatic hydrocarbon, and most of the quenching oil KGS is vaporized in the separation/fractionation section S50 into the flash gas of the base stream MCP-CS, so that the heat absorbed in the cooling-down stabilizing section DT10 is brought into the flash gas of the base stream MCP-CS to be utilized, and during the condensation of the flash gas of the base stream MCP-CS, the vapor phase component from the quenching oil KGS mostly completes the condensation process to release heat.

2. The method according to claim 1, wherein:

in the heavy oil suspension bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with the conventional boiling point higher than 530 ℃ in the heavy oil R10F is higher than 50%;

the method comprises the steps of performing hydroconversion on heavy oil R10 and heavy oil R10F in a reaction part R10 of heavy oil suspension bed, wherein the weight concentration of hydrocarbon components with conventional boiling points higher than 530 ℃ is higher than 70%, and at the same time at least one of the following conditions is satisfied:

(1) asphaltene weight concentration greater than 12%;

(2) the Kangshi carbon residue value is higher than 16%;

(3) the weight content of organic sulfur is higher than 0.5%;

(4) the organic nitrogen weight content is higher than 0.15%;

(5) the weight content of the organic metal is higher than 0.015%;

in the cooling stabilizing section DT10, an asphaltene-containing material flow MCP containing hydrocarbon components with a conventional boiling point lower than 530 ℃ and hydrocarbon components with a conventional boiling point higher than 530 ℃ based on a reaction product R10P is mixed with quenching oil KGS to form a quenched mixture material flow MCP-BASE;

in the cooling stabilizing part DT10, a material flow MCP with the temperature of T1 is mixed with quenching oil KGS with the temperature of T3 to form a quenched mixture material flow MCP-BASE with the temperature of T2, the cooling amplitude of the material flow MCP is DT, DT=T1-T2, and DT is 15-80 ℃;

a stream MCP selected from one or more of the following streams:

(1) The reaction product R10P, serves as a crop stream MCP;

(2) thermal high-split oil S10-L, used as stream MCP;

(3) the hot high-pressure oil S10-L forms a vapor-liquid mixed phase material after depressurization, and the vapor-liquid mixed phase material is used as a crop stream MCP;

(4) the vapor-liquid mixed phase material formed by the hot high-pressure oil S10-L after depressurization is separated into primary hot low-pressure flash steam and primary hot low-pressure flash oil in the primary hot low-pressure flash evaporation process; the operating pressure of the primary hot low pressure flash process is greater than atmospheric pressure;

a first stage hot low pressure flash oil, used as stream MCP;

(5) the vapor-liquid mixed phase material formed by the hot high-pressure oil S10-L after depressurization is separated into primary hot low-pressure flash steam and primary hot low-pressure flash oil in the primary hot low-pressure flash evaporation process; the operating pressure of the primary hot low pressure flash process is greater than atmospheric pressure;

after the primary heat low pressure flash oil is depressurized, separating the primary heat low pressure flash oil into secondary heat low pressure flash steam and secondary heat low pressure flash oil in a secondary heat low pressure flash process; the operating pressure of the secondary hot low pressure flash process is greater than atmospheric pressure;

a second stage hot low pressure flash oil, used as stream MCP;

(6) the vapor-liquid mixed phase material formed by the hot high-pressure oil S10-L after depressurization is separated into hot low-pressure flash steam and hot low-pressure flash oil in a hot low-pressure flash evaporation process, and the operating pressure of the hot low-pressure flash evaporation process is higher than the atmospheric pressure;

The hot low-pressure flash oil enters a flash evaporation process of negative pressure operation after depressurization, and the operation pressure of the hot low-pressure flash oil entering a negative pressure operation state after depressurization is greater than the atmospheric pressure and is used as a crop stream MCP.

3. The method according to claim 1, wherein:

in the heavy oil suspension bed hydroconversion process U100, the hydrocracking weight conversion rate of hydrocarbon components with the conventional boiling point higher than 530 ℃ in the heavy oil R10F is higher than 50%;

in a reaction part R10 of heavy oil suspension bed hydroconversion, under the conditions that hydrogen, conventional liquid hydrocarbon and solid particle catalyst R10-CAT for heavy oil suspension bed hydroconversion exist, hydrogen-supplying hydrocarbon exists or other solid particles exist or mixed phase materials exist, heavy oil R10F is subjected to heavy oil suspension bed hydroconversion reaction R10R containing suspension bed hydrocracking reaction to be converted into reaction product R10P;

the solid particle catalyst R10-CAT at least comprises Mo element, and the main working form of Mo in the reaction part R10 is M0S2;

heavy oil R10F having a conventional boiling point greater than 530 ℃ and a hydrocarbon component weight concentration greater than 70%, while satisfying at least one of the following conditions:

(1) asphaltene weight concentration greater than 12%;

(2) the Kangshi carbon residue value is higher than 16%;

(3) The weight content of organic sulfur is higher than 0.5%;

(4) the organic nitrogen weight content is higher than 0.15%;

(5) the weight content of the organic metal is higher than 0.015%;

in the reaction part R10, the weight conversion per hydrocracking pass of the hydrocarbon components with the conventional boiling point higher than 530 ℃ in the whole raw oil is higher than 20 percent, so that at least 50 weight percent of asphaltenes in the heavy oil R10F complete the hydrocracking reaction; all of the feedstock oil from reaction section R10, including heavy oil R10F and recycle vacuum flash oil S50-FL-TOR10 from the vacuum flash bottom oil recycle section;

the heavy oil suspension bed hydro-conversion reaction R10R comprises a suspension bed hydro-refining reaction, wherein at least 80 weight percent of organic metal in the heavy oil R10F is subjected to hydro-demetallization reaction, at least 60 weight percent of organic sulfur in the heavy oil R10F is subjected to hydro-desulfurization reaction, at least 30 weight percent of organic nitrogen in the heavy oil R10F is subjected to hydro-denitrification reaction, and the average Conn carbon residue value of all conventional liquid hydrocarbons in a reaction product R10P is lower than 50 percent of the average Conn carbon residue value of the heavy oil R10F;

in the hot high pressure separation section S10, an asphaltene-containing stream comprising hydrocarbon components having a conventional boiling point above 530 ℃ based on the reaction product R10P is separated into a hot high-pressure gas S10-V and a hot high-pressure oil S10-L;

In the cooling stabilizing section DT10, an asphaltene-containing material flow MCP containing hydrocarbon components with a conventional boiling point lower than 530 ℃ and hydrocarbon components with a conventional boiling point higher than 530 ℃ based on a reaction product R10P is mixed with quenching oil KGS to form a quenched mixture material flow MCP-BASE;

an asphaltene-containing stream comprising hydrocarbon components having conventional boiling points above 530 ℃ based on the quenched mixture stream MCP-BASE as a BASE stream MCP-CS;

a third separation/fractionation section S50 comprising at least a reduced pressure flash step;

in the separation/fractionation section S50, the base stream MCP-CS flashes off the vapor MCP-CS-FV composed of the low boiling components LCOM to obtain a reduced pressure flash bottoms S50-FL containing asphaltene-containing solid particulate catalyst R10-CAT containing hydrocarbon components having a conventional boiling point above 530 ℃;

at least one part of the material containing asphaltene and containing solid particle catalyst R10-CAT, which is based on hydrocarbon components with the conventional boiling point higher than 530 ℃ and mainly comprises the pressure-reduced flash evaporation bottom oil S50-FL, is used as the pressure-reduced flash evaporation bottom oil S50-FL-OUT;

the weight flow rate of the hydrocarbon component with the conventional boiling point higher than 530 ℃ in the discharged reduced pressure flash bottom oil S50-FL-OUT is lower than 50% of the weight flow rate of the hydrocarbon component with the conventional boiling point higher than 530 ℃ in the heavy oil R10F;

Fifthly, in a reduced pressure flash evaporation bottom oil circulation part, at least one part of materials containing solid particle catalyst R10-CAT which mainly consists of hydrocarbon components with the conventional boiling point higher than 530 ℃ based on reduced pressure flash evaporation bottom oil S50-FL is returned to the reaction part R10 as circulating reduced pressure flash evaporation oil S50-FL-TOR 10;

in the reaction part R10, the circulating vacuum flash oil S50-FL-TOR10 or the intermediate hydrogenation product of the circulating vacuum flash oil S50-FL-TOR10 is mixed and contacted with heavy oil R10F or the intermediate hydrogenation product of heavy oil R10F;

in the quenching oil supply part K100, the quenching oil KGS is one or more of the following oils:

(1) in the separation/fractionation section S50, the initial quench oil KGS0 comes from a positive pressure fractionation process, mainly consisting of diesel components, the initial quench oil KGS0 having a temperature of 180-280 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS 0;

(2) in the separation/fractionation section S50, the initial quench oil KGS0 comes from a negative pressure fractionation process, mainly consisting of wax oil components, the initial quench oil KGS0 having a temperature of 130-270 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS 0;

(3) hydrocarbon streams containing waxy oil components consisting essentially of diesel components based on cold high-fraction oils.

4. A method according to claim 3, characterized in that:

in the heavy oil suspension bed hydro-conversion process U100, the weight conversion rate of the hydro-cracking of the hydrocarbon component with the conventional boiling point higher than 530 ℃ in the heavy oil R10F is 75-98 percent;

the method comprises the steps that in a reaction part R10, the weight content of M0S2 in a liquid phase in a reaction process is 0.1-0.5%;

heavy oil R10F having a conventional boiling point greater than 530 ℃ and a hydrocarbon component weight concentration greater than 85%, while satisfying at least one of the following conditions:

(1) asphaltene weight concentration greater than 16%;

(2) the Kangshi carbon residue value is higher than 24%;

(3) the weight content of organic sulfur is higher than 2.5%;

(4) the organic nitrogen weight content is higher than 0.25%;

(5) the weight content of the organic metal is higher than 0.025%;

the operating conditions of the reaction section R10 are: the temperature is 380-460 ℃, the pressure is 8.0-25.0 MPa, the volume ratio of hydrogen to raw oil is 50-4000, and the volume airspeed is 0.1-10.0 hr ^-1 The method comprises the steps of carrying out a first treatment on the surface of the The weight chemical hydrogen consumption of heavy oil R10F is 0.05-4.00%;

the operating conditions of the thermal high pressure separation section S10 are: the temperature is 360-460 ℃ and the pressure is 8.0-25.0 MPa, and stripping hydrogen is injected or not injected into a hot high-pressure oil S10-L liquid phase region;

in the cooling stabilizing section DT10, an asphaltene-containing material flow MCP containing hydrocarbon components with a conventional boiling point lower than 530 ℃ and hydrocarbon components with a conventional boiling point higher than 530 ℃ based on a reaction product R10P is mixed with quenching oil KGS to form a quenched mixture material flow MCP-BASE;

In the cooling stabilizing part DT10, a material flow MCP with the temperature of T1 is mixed with quenching oil KGS with the temperature of T3 to form a quenched mixture material flow MCP-BASE with the temperature of T2, the cooling amplitude of the material flow MCP is DT, DT=T1-T2, and DT is 25-75 ℃;

the ratio of the weight flow rate of the quenching oil KGS to the weight flow rate of the stream MCP is 0.01-0.65;

a third separation/fractionation section S50 comprising at least a reduced pressure flash step;

in the separation/fractionation section S50, the base stream MCP-CS flashes off the vapor MCP-CS-FV composed of the low boiling components LCOM to obtain a reduced pressure flash bottoms S50-FL containing asphaltene-containing solid particulate catalyst R10-CAT containing hydrocarbon components having a conventional boiling point above 530 ℃;

the gas MCP-CS-FV composed of the low boiling point component LCOM enters a separation recovery system S50-VD to be separated and recovered;

at least one part of the material containing asphaltene and containing solid particle catalyst R10-CAT, which is based on hydrocarbon components with the conventional boiling point higher than 530 ℃ and mainly comprises the pressure-reduced flash evaporation bottom oil S50-FL, is used as the pressure-reduced flash evaporation bottom oil S50-FL-OUT;

the ratio of the weight flow rate of the conventional hydrocarbon components with boiling points higher than 530 ℃ in the discharged reduced pressure flash bottoms S50-FL-OUT to the weight flow rate of the conventional hydrocarbon components with boiling points higher than 530 ℃ in the heavy oil R10F is lower than 25%;

And fifthly, in the reduced pressure flash evaporation bottom oil circulation part, the ratio of the weight flow rate of the circulating reduced pressure flash evaporation oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 0.5-2.0.

5. A method according to claim 3, characterized in that:

in the heavy oil suspension bed hydro-conversion process U100, the weight conversion rate of the hydro-cracking of the hydrocarbon component with the conventional boiling point higher than 530 ℃ in the heavy oil R10F is 88-95 percent;

in the reaction part R10, M0S in the liquid phase of the reaction process ₂ The weight content is 0.2-0.4%;

heavy oil R10F having a conventional boiling point greater than 530 ℃ and a hydrocarbon component weight concentration greater than 90% while satisfying at least one of the following conditions:

(1) asphaltene weight concentration greater than 20%;

(2) the Kangshi carbon residue value is higher than 28%;

(3) the weight content of organic sulfur is higher than 3.5%;

(4) the organic nitrogen weight content is higher than 0.45%;

(5) the weight content of the organic metal is higher than 0.050%;

the operating conditions of the reaction section R10 are: the temperature is 400-440 ℃, the pressure is 10.0-17.0 MPa, the volume ratio of hydrogen to raw oil is 100-1500, the volume airspeed is 0.2-2.0 hr ^-1 The method comprises the steps of carrying out a first treatment on the surface of the The weight chemical hydrogen consumption of heavy oil R10F is 2.00-3.50%;

the operating conditions of the thermal high pressure separation section S10 are: the temperature is 360-440 ℃, the pressure is 10.0-17.0 MPa, and stripping hydrogen is injected or not injected into a hot high-pressure oil S10-L liquid phase region;

In the cooling stabilizing section DT10, an asphaltene-containing material flow MCP containing hydrocarbon components with a conventional boiling point lower than 530 ℃ and hydrocarbon components with a conventional boiling point higher than 530 ℃ based on a reaction product R10P is mixed with quenching oil KGS to form a quenched mixture material flow MCP-BASE;

in the cooling stabilizing part DT10, a material flow MCP with the temperature of T1 is mixed with quenching oil KGS with the temperature of T3 to form a quenched mixture material flow MCP-BASE with the temperature of T2, the cooling amplitude of the material flow MCP is DT, DT=T1-T2, and DT is 35-65 ℃;

the ratio of the weight flow rate of the quenching oil KGS to the weight flow rate of the stream MCP is 0.01-0.65;

a third separation/fractionation section S50 comprising at least a reduced pressure flash step;

in the separation/fractionation section S50, the base stream MCP-CS flashes off the vapor MCP-CS-FV composed of the low boiling components LCOM to obtain a reduced pressure flash bottoms S50-FL containing asphaltene-containing solid particulate catalyst R10-CAT containing hydrocarbon components having a conventional boiling point above 530 ℃;

the gas MCP-CS-FV composed of the low boiling point component LCOM enters a separation recovery system S50-VD to be separated and recovered;

at least one part of the material containing asphaltene and containing solid particle catalyst R10-CAT, which is based on hydrocarbon components with the conventional boiling point higher than 530 ℃ and mainly comprises the pressure-reduced flash evaporation bottom oil S50-FL, is used as the pressure-reduced flash evaporation bottom oil S50-FL-OUT;

The ratio of the weight flow rate of the conventional hydrocarbon components with boiling points higher than 530 ℃ in the discharged reduced pressure flash bottoms S50-FL-OUT to the weight flow rate of the conventional hydrocarbon components with boiling points higher than 530 ℃ in the heavy oil R10F is lower than 12%;

and fifthly, in the reduced pressure flash evaporation bottom oil circulation part, the ratio of the weight flow rate of the circulating reduced pressure flash evaporation oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 1.0-2.0.

6. The method according to claim 2, characterized in that:

heavy oil R10F, selected from one or several of the following streams:

(1) a base oil of a crude oil reduced pressure distillation process;

(2) base oil in the shale oil reduced pressure distillation process;

(3) base oil of oil sand oil reduced pressure distillation process;

(4) base oil in the coal tar reduced pressure distillation process;

(5) solvent deasphalted oil.

7. The method according to claim 2, characterized in that:

the quenching oil KGS is one or more of the following oils:

(1) separating the flash vapors of the base stream MCP-CS in a separation/fractionation section S50 to obtain a condensed oil;

(2) hydrocarbon streams containing waxy oil components consisting essentially of diesel components based on cold high-fraction oils.

8. The method according to claim 2, characterized in that:

thirdly, in a separation/fractionation part S50, reducing the pressure of the hot high-pressure separated oil S10-L to obtain a mixed-phase material S10-L-DP;

The mixed phase material S10-L-DP enters a first thermal low-pressure flash evaporation process and is separated into first thermal low-pressure gas and first thermal low-pressure oil; the operating conditions of the first hot low pressure flash process were: the temperature is 340-440 ℃ and the pressure is 0.35-2.0 MPa; the first hot low-split oil is contacted with or without stripping steam;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil;

the operating conditions of the second hot low pressure flash process were: the temperature is 330-430 ℃ and the pressure is 0.15-0.30 MPa; the second hot low-split oil is contacted with or without stripping steam; the operating pressure of the second thermal low pressure flash process is lower than the operating pressure of the first thermal low pressure flash process;

the second thermal low-pressure oil separation is depressurized and then enters a first negative pressure flash evaporation process to be separated into first negative pressure flash vapor and first negative pressure flash oil; the operating conditions of the first negative pressure flash process are: the temperature is 325-415 ℃, and the pressure is minus 0.55-minus 0.098MPa; the first negative pressure flash oil is contacted with or without stripping water vapor; the operating pressure of the first negative pressure flash process is lower than the operating pressure of the second hot low pressure flash process;

the first negative pressure flash oil is used as a reduced pressure flash bottom oil S50-FL;

The first hot low-pressure gas enters or does not enter the first hot low-pressure gas rectification process for separation;

the second hot low-pressure gas enters or does not enter the second hot low-pressure gas rectification process for separation;

the first thermal low-pressure gas-separating rectification process and the second thermal low-pressure gas-separating rectification process are respectively provided with or share one set of rectification process;

the first negative pressure flash steam enters or does not enter the first negative pressure flash steam rectification process for separation;

the flash steam of the first thermal low-pressure flash process is directly discharged into the first thermal low-pressure flash process or is mixed and contacted with liquid from the first thermal low-pressure gas separation rectification process to be discharged into the first thermal low-pressure flash process

The flash steam of the second thermal low-pressure flash process is directly discharged into the second thermal low-pressure flash process or is mixed with liquid from the second thermal low-pressure fractional gas rectification process to be discharged into the second thermal low-pressure flash process

The flash steam of the first negative pressure flash evaporation process is directly discharged out of the first negative pressure flash evaporation process, or is discharged out of the first negative pressure flash evaporation process after being mixed and contacted with liquid from the first negative pressure flash evaporation process.

9. The method according to claim 2, characterized in that:

thirdly, in a separation/fractionation part S50, reducing the pressure of the hot high-pressure separated oil S10-L to obtain a mixed-phase material S10-L-DP;

The mixed phase material S10-L-DP enters a first thermal low-pressure flash evaporation process and is separated into first thermal low-pressure gas and first thermal low-pressure oil; the operating conditions of the first hot low pressure flash process were: the temperature is 340-440 ℃ and the pressure is 0.35-2.0 MPa; the first hot low-split oil is contacted with or without stripping steam;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil;

the operating conditions of the second hot low pressure flash process were: the temperature is 330-430 ℃ and the pressure is 0.15-0.30 MPa; the second hot low-split oil is contacted with or without stripping steam; the operating pressure of the second thermal low pressure flash process is lower than the operating pressure of the first thermal low pressure flash process;

the second thermal low-pressure oil separation is depressurized and then enters a first negative pressure flash evaporation process to be separated into first negative pressure flash vapor and first negative pressure flash oil; the operating conditions of the first negative pressure flash process are: the temperature is 325-415 ℃, and the pressure is minus 0.55-minus 0.098MPa; the first negative pressure flash oil is contacted with or without stripping water vapor; the operating pressure of the first negative pressure flash process is lower than the operating pressure of the second hot low pressure flash process;

the first negative pressure flash oil is depressurized and then enters a second negative pressure flash process to be separated into second negative pressure flash steam and second negative pressure flash oil; the operating conditions of the second negative pressure flash process are: the temperature is 345-405 ℃ and the pressure is minus 0.090 to minus 0.098MPa; contacting the second hot low-split oil with or without stripping steam; the operating pressure of the second negative pressure flash process is lower than the operating pressure of the first negative pressure flash process;

The second negative pressure flash oil is used as a reduced pressure flash bottom oil S50-FL;

the first hot low-pressure gas enters or does not enter the first hot low-pressure gas rectification process for separation;

the second hot low-pressure gas enters or does not enter the second hot low-pressure gas rectification process for separation;

the first thermal low-pressure gas-separating rectification process and the second thermal low-pressure gas-separating rectification process are respectively provided with or share one set of rectification process;

the first negative pressure flash steam enters or does not enter the first negative pressure flash steam rectification process for separation;

the second negative pressure flash steam enters or does not enter the second negative pressure flash steam rectification process for separation;

the first negative pressure flash steam rectification process and the second negative pressure flash steam rectification process are respectively provided with or share one set of rectification process;

the flash steam of the first thermal low-pressure flash process is directly discharged into the first thermal low-pressure flash process or is mixed and contacted with liquid from the first thermal low-pressure gas separation rectification process to be discharged into the first thermal low-pressure flash process

The flash steam of the second thermal low-pressure flash process is directly discharged into the second thermal low-pressure flash process or is mixed with liquid from the second thermal low-pressure fractional gas rectification process to be discharged into the second thermal low-pressure flash process

The flash steam of the first negative pressure flash evaporation process is directly discharged from the first negative pressure flash evaporation process, or is discharged from the first negative pressure flash evaporation process after being mixed and contacted with liquid from the first negative pressure flash evaporation process;

The flash steam of the second negative pressure flash evaporation process is directly discharged out of the second negative pressure flash evaporation process, or is mixed and contacted with liquid from the second negative pressure flash evaporation process and then discharged out of the second negative pressure flash evaporation process.

10. The method according to claim 8 or 9, characterized in that:

and (3) enabling the rectified bottom oil discharged from the rectification process of the flash steam in the first thermal low-pressure flash evaporation process and/or the rectified bottom oil discharged from the rectification process of the flash steam in the second thermal low-pressure flash evaporation process to enter the first thermal low-pressure flash evaporation process and/or the second thermal low-pressure flash evaporation process, and enabling the rectified bottom oil to be in mixed contact with the flash steam in the first thermal low-pressure flash evaporation process and/or the flash steam in the second thermal low-pressure flash evaporation process to serve as washing oil for washing heavy components and solid particles in the flash steam.

11. The method according to claim 8 or 9, characterized in that:

the rectification bottom oil discharged from the rectification process of the flash steam of the first negative pressure flash evaporation process and/or the rectification bottom oil discharged from the rectification process of the flash steam of the second negative pressure flash evaporation process enter the first negative pressure flash evaporation process and/or the second negative pressure flash evaporation process, and are mixed and contacted with the flash steam of the first negative pressure flash evaporation process and/or the flash steam of the second negative pressure flash evaporation process to be used as washing oil for washing heavy components and solid particles in the flash steam.

12. The method according to claim 8 or 9, characterized in that:

and the liquid flow of the wax-containing oil component discharged from the negative pressure rectification process of the flash steam of the negative pressure flash evaporation process enters the first thermal low-pressure flash evaporation process and/or the second thermal low-pressure flash evaporation process, and is mixed and contacted with the flash steam of the first thermal low-pressure flash evaporation process and/or the flash steam of the second thermal low-pressure flash evaporation process to serve as washing oil to wash heavy components and solid particles in the flash steam.

13. The method according to claim 8 or 9, characterized in that:

and (3) a liquid phase hydrocarbon oil stream containing wax oil and not containing vacuum residuum, which is obtained in the rectification process of flash steam in the first thermal low-pressure flash evaporation process and/or the rectification process of flash steam in the second thermal low-pressure flash evaporation process, enters the negative pressure rectification process of flash steam in the negative pressure flash evaporation process and is used as intermediate feed.

14. The method according to claim 2, characterized in that:

third, in the separation/fractionation part S50, the gas MCP-CS-FV composed of the low boiling point component LCOM enters a separation recovery system S50-VD to be separated and recovered;

heating initial quenching oil KGS0 from a quenching oil supply part K100 in an indirect heating step HX6030 based on heat released in the condensation process of the gas MCP-CS-FV in a separation recovery system S50-VD to obtain preheated initial quenching oil KGS0-H, wherein a stream based on the preheated initial quenching oil KGS0-H is used as quenching oil KGS to enter a cooling stabilizing part DT10;

The composition of the components of the quenching oil KGS is the same as or different from the composition of the components of the initial quenching oil KGS0, and the weight flow rate of the quenching oil KGS is the same as or different from the weight flow rate of the initial quenching oil KGS0; a process of pre-heating the initial quench oil KGS0 to a post-pre-heating initial quench oil KGS0-H, with or without a flash process, with or without a fractionation process;

providing initial quenching oil KGS0 in a quenching oil supply part K100;

the initial quenching oil KGS0 is condensed oil obtained by separating flash evaporation gas of a basic stream MCP-CS in a separation/fractionation part S50, and the condensed oil is preheated in an indirect heating step HX6030 in the separation/fractionation part S50 to obtain quenching oil KGS;

the initial quench oil KGS0 is one or several of the following oils:

(1) in the separation/fractionation section S50, the initial quench oil KGS0 comes from a positive pressure fractionation process, mainly consisting of diesel components, the initial quench oil KGS0 having a temperature of 180-280 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS0;

(2) in the separation/fractionation section S50, the initial quench oil KGS0 comes from a negative pressure fractionation process, mainly consisting of wax oil components, the initial quench oil KGS0 having a temperature of 130-270 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS0;

(3) Hydrocarbon streams containing waxy oil components consisting essentially of diesel components based on cold high-fraction oils.

15. The method according to claim 14, wherein:

and thirdly, in the separation/fractionation part S50, in normal operation, the oil-free heating furnace is not arranged for heating, or the heating furnace through which oil passes is not arranged for heating.

16. The method according to claim 15, wherein:

and fifthly, in the reduced pressure flash evaporation bottom oil circulation part, the ratio of the weight flow rate of the circulating reduced pressure flash evaporation oil S50-FL-TOR10 to the weight flow rate of the heavy oil R10F is 1.0-2.0.

17. The method according to claim 2, characterized in that:

in the cooling stabilizing section DT10, an asphaltene-containing stream MCP based on the hot high-fraction oil S10-L and containing hydrocarbon components with conventional boiling points higher than 530 ℃ is mixed with the quenching oil KGS based on the separation/fractionation section S50 to form a base stream MCP-CS;

third, in the separation/fractionation part S50, the gas MCP-CS-FV composed of the low boiling point component LCOM enters a separation recovery system S50-VD to be separated and recovered;

heating initial quenching oil KGS0 in an indirect heating step HX6030 based on heat released in the condensation process of gas MCP-CS-FV in a separation recovery system S50-VD to obtain preheated initial quenching oil KGS0-H, wherein a stream based on the preheated initial quenching oil KGS0-H is used as quenching oil KGS to enter a cooling stabilizing part DT10;

The composition of the components of the quenching oil KGS is the same as or different from the composition of the components of the initial quenching oil KGS0, and the weight flow rate of the quenching oil KGS is the same as or different from the weight flow rate of the initial quenching oil KGS0; a process for preheating the initial quench oil KGS0 to a preheated initial quench oil KGS0-H, with or without flash distillation process KGSO-FPR, with or without fractionation process KGSO-DPR;

the flash steam of the flash evaporation process KGSO-FPR and/or the steam product of the fractionation process KGSO-DPR enter or not enter a separation recovery system S50-VD of the steam MCP-CS-FV;

providing initial quenching oil KGS0 in a quenching oil supply part K100;

the initial quenching oil KGS0 is preheated by an indirect heating step HX6030 in a separation/fractionation part S50 to obtain quenching oil KGS;

the initial quench oil KGS0 is one or several of the following oils:

(1) in the separation/fractionation section S50, the initial quench oil KGS0 comes from a positive pressure fractionation process, mainly consisting of diesel components, the initial quench oil KGS0 having a temperature of 180-280 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS0;

(2) in the separation/fractionation section S50, the initial quench oil KGS0 comes from a negative pressure fractionation process, mainly consisting of wax oil components, the initial quench oil KGS0 having a temperature of 130-270 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS0;

(3) Hydrocarbon streams containing waxy oil components consisting essentially of diesel components based on cold high-fraction oils.

18. The method according to claim 17, wherein:

third, in the separation/fractionation part S50, the gas MCP-CS-FV composed of the low boiling point component LCOM enters a separation recovery system S50-VD to be separated and recovered;

heating initial quenching oil KGS0 in an indirect heating step HX6030 based on heat released in the condensation process of gas MCP-CS-FV in a separation recovery system S50-VD to obtain preheated initial quenching oil KGS0-H, wherein a stream based on the preheated initial quenching oil KGS0-H is used as quenching oil KGS to enter a cooling stabilizing part DT10;

and an indirect heating step HX6030 of converting the initial quenching oil KGS0 into preheated initial quenching oil KGS0-H, wherein at least 2 serially connected preheating processes are used, the initial quenching oil KGS0 is subjected to a flash evaporation operation after an upstream preheating process to obtain a liquid with gas removed, the liquid enters an adjacent downstream preheating process, and finally the liquid discharged from the indirect heating step HX6030 after the preheating of the initial quenching oil KGS0-H after the flash evaporation to remove the gas KGS0-H-V is used as the quenching oil KGS.

19. The method according to claim 18, wherein:

in the indirect heating step HX6030, the steam KGS0-H-V enters a fractionating tower of a separation recovery system S50-VD of the steam MCP-CS-FV.

20. The method according to claim 17 or 18 or 19, characterized in that:

from the separation/fractionation section S50, the initial quench oil KGS0 comes from a positive pressure fractionation process, mainly consisting of diesel components, the initial quench oil KGS0 having a temperature of 180-280 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS 0.

21. The method according to claim 17 or 18 or 19, characterized in that:

from the separation/fractionation section S50, the initial quench oil KGS0 comes from a sub-atmospheric fractionation process, mainly consisting of wax oil components, the initial quench oil KGS0 having a temperature of 130-270 ℃ and the quench oil KGS having a temperature at least 40 ℃ higher than the initial quench oil KGS 0.

22. The method according to claim 1, wherein:

the hydrogen-supplying hydrocarbon is used in a reaction part R10 of hydro-conversion of a heavy oil suspension bed.

23. The method according to claim 2, characterized in that:

in the cooling stabilizing section DT10, an asphaltene-containing stream MCP based on the hot high-fraction oil S10-L containing hydrocarbon components with a conventional boiling point higher than 530 ℃ is mixed with the quench oil KGS from the separation/fractionation section S50 to form a base stream MCP-CS;

third, in the separation/fractionation part S50, the gas MCP-CS-FV composed of the low boiling point component LCOM enters a separation recovery system S50-VD to be separated and recovered;

Heating initial quenching oil KGS0 in an indirect heating step HX6030 based on heat released in the condensation process of gas MCP-CS-FV in a separation recovery system S50-VD to obtain preheated initial quenching oil KGS0-H, wherein a stream based on the preheated initial quenching oil KGS0-H is used as quenching oil KGS to enter a cooling stabilizing part DT10;

in the quench oil supply section K100, the initial quench oil KGS0 is a condensate BASE-KGS0 obtained by separating the flash vapors of the BASE stream MCP-CS in the separation/fractionation section S50, and the distillate BASE-KGS0 is used as the quench oil KGS after the pressure is increased and the temperature is increased.

24. The method according to claim 23, wherein:

the temperature of the initial quenching oil KGS0 is 110-200 ℃ and the temperature of the quenching oil KGS is 230-300 ℃ when the separation/fractionation of the part S50 is carried out.

25. The method according to claim 23, wherein:

the temperature of the initial quenching oil KGS0 is 130-180 ℃ and the temperature of the quenching oil KGS is 260-290 ℃ when the separation/fractionation of the part S50 is carried out.

26. The method according to claim 23, wherein:

in the cooling stabilizing part DT10, the ratio of the weight flow of the quenching oil KGS to the weight flow of the stream MCP is 0.01-0.15 or 0.15-0.30 or 0.30-0.45 or more than 0.45.

27. The method according to claim 2, characterized in that:

in a quenching oil supply part K100, the quenching oil KGS is circulating oil;

the quenching oil KGS is condensed oil obtained by separating flash vapors of the base stream MCP-CS in a separation/fractionation section S50;

a base stream MCP-CS selected from one or more of the following streams:

(1) the mixed phase material flow formed by reducing the pressure of the hot high-pressure separated oil S10-L is used as a material flow MCP, and is mixed with the quenching oil KGS to form a base material flow MCP-CS;

(2) the mixed phase material flow formed by depressurization of the thermal high-pressure oil S10-L enters a first thermal low-pressure flash evaporation process and is separated into first thermal low-pressure gas and first thermal low-pressure oil, and the first thermal low-pressure oil is used as material flow MCP; the first hot low pressure flash process operating pressure is greater than atmospheric pressure;

mixing the material flow MCP with the quenching oil KGS to form a base material flow MCP-CS;

(3) the mixed phase material flow formed by depressurization of the thermal high-pressure oil S10-L enters a first thermal low-pressure flash evaporation process and is separated into first thermal low-pressure gas and first thermal low-pressure oil, and the first thermal low-pressure oil is used as material flow MCP; the first hot low pressure flash process operating pressure is greater than atmospheric pressure;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil, and the second thermal low-pressure oil is used as a material flow MCP; the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

Mixing the material flow MCP with the quenching oil KGS to form a base material flow MCP-CS;

(4) the mixed phase material flow formed by depressurization of the thermal high-pressure oil S10-L enters a first thermal low-pressure flash evaporation process and is separated into first thermal low-pressure gas and first thermal low-pressure oil, and the first thermal low-pressure oil is used as material flow MCP; the first hot low pressure flash process operating pressure is greater than atmospheric pressure;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil;

the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

the second thermal low-pressure oil is separated into first negative pressure flash steam and first negative pressure flash oil in a first negative pressure flash process, and the first negative pressure flash oil is used as a material flow MCP;

mixing the material flow MCP with the quenching oil KGS to form a base material flow MCP-CS;

in the second negative pressure flash evaporation process, separating the base material flow MCP-CS into second negative pressure flash steam and second negative pressure flash oil; the operating pressure of the second negative pressure flash process is lower than the operating pressure of the first negative pressure flash process;

separating condensed oil obtained by the second negative pressure flash steam to be used as quenching oil KGS.

28. The method according to claim 2, characterized in that:

In a quenching oil supply part K100, the quenching oil KGS is circulating oil;

in the quenching oil supply part K100, the mixed phase stream formed by depressurization of the hot high-pressure separation oil S10-L is taken as a stream MCP, and is mixed with the quenching oil KGS to form a base stream MCP-CS;

the quenching oil KGS is condensed oil obtained by separating flash vapors of the base stream MCP-CS in a separation/fractionation section S50;

and the quenching oil KGS is selected from one or more of the following streams:

(1) the base material flow MCP-CS enters a first hot low pressure flash evaporation process and is separated into first hot low-pressure gas and first hot low-pressure oil;

separating the condensed oil from the first hot low-pressure gas fraction in separation/fractionation section S50 as quench oil KGS;

(2) the base material flow MCP-CS enters a first hot low pressure flash evaporation process and is separated into first hot low-pressure gas and first hot low-pressure oil; the first hot low pressure flash process operating pressure is greater than atmospheric pressure;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil;

the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

the second heat low-pressure gas enters a separation and/or fractionation process of the first heat low-pressure gas to be recovered in a combined way;

Separating the condensed oil from the first hot low-pressure gas fraction in separation/fractionation section S50 as quench oil KGS;

(3) the base material flow MCP-CS enters a first hot low pressure flash evaporation process and is separated into first hot low-pressure gas and first hot low-pressure oil; the first hot low pressure flash process operating pressure is greater than atmospheric pressure;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil;

the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

the second thermal low-pressure oil is separated into first negative pressure flash steam and first negative pressure flash oil in the first negative pressure flash process;

separating the condensate oil from the first negative pressure flash gas in separation/fractionation section S50 as quench oil KGS;

(4) the base material flow MCP-CS enters a first hot low pressure flash evaporation process and is separated into first hot low-pressure gas and first hot low-pressure oil; the first hot low pressure flash process operating pressure is greater than atmospheric pressure;

the first thermal low-pressure oil is depressurized and then enters a second thermal low-pressure flash evaporation process to be separated into second thermal low-pressure gas and second thermal low-pressure oil;

the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

The second thermal low-pressure oil is separated into first negative pressure flash steam and first negative pressure flash oil in the first negative pressure flash process;

the first negative pressure flash oil is separated into second negative pressure flash steam and second negative pressure flash oil in a second negative pressure flash process; the operating pressure of the second negative pressure flash process is lower than the operating pressure of the first negative pressure flash process;

the second negative pressure flash steam enters a separation and/or fractionation process of the first negative pressure flash steam to be recovered in a combined way;

the condensate oil obtained from the first negative pressure flash gas is separated in the separation/fractionation section S50 as the quench oil KGS.

29. The method according to claim 2, characterized in that:

the sixth step of introducing a material flow subjected to depressurization of the hot high-pressure oil S10-L into a first hot low-pressure flash evaporation process in a quenching oil supply part K100 to be separated into first hot low-pressure gas and first hot low-pressure oil; the first hot low pressure flash process operating pressure is greater than atmospheric pressure; the first thermal bottoms oil is taken as stream MCP;

mixing the material flow MCP with the quenching oil KGS to form a base material flow MCP-CS;

a portion of the base oil cooled stream resulting from the flash evaporation process based on the base stream MCP-CS is used as the quench oil KGS, selected from one or more of the following streams:

(1) the base material flow MCP-CS enters a second thermal low-pressure flash evaporation process and is separated into second thermal low-pressure gas and second thermal low-pressure oil; the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

The second heat low-pressure gas enters a separation and/or fractionation process of the first heat low-pressure gas to be recovered in a combined way;

separating the condensed oil from the first hot low-pressure gas fraction in separation/fractionation section S50 as quench oil KGS;

(2) the base material flow MCP-CS enters a second thermal low-pressure flash evaporation process and is separated into second thermal low-pressure gas and second thermal low-pressure oil; the second hot low pressure flash process operating pressure is greater than atmospheric pressure; the second thermal low pressure flash process operating pressure is lower than the first thermal low pressure flash process operating pressure;

the second thermal low-pressure oil is separated into first negative pressure flash steam and first negative pressure flash oil in the first negative pressure flash process;

the first negative pressure flash steam enters a separation and/or fractionation process of the first negative pressure flash steam for recovery;

the condensate oil obtained from the first negative pressure flash gas is separated in the separation/fractionation section S50 as the quench oil KGS.

30. The method according to claim 2, characterized in that:

in the cooling stabilizing part DT10, an asphaltene-containing material flow MCP00 containing hydrocarbon components with the conventional boiling point lower than 530 ℃ and hydrocarbon components with the conventional boiling point higher than 530 ℃ based on a reaction product R10P is split into 2 paths of material flows MCP01 and MCP02, the material flow MCP01 is used as a first path of characteristic material flow for separating to obtain circulating vacuum flash oil S50-FL-TOR10, and the material flow MCP02 is used as a second path of characteristic material flow for separating to obtain discharged vacuum flash bottom oil S50-FL-OUT;

The first characteristic flow MCP01 is mixed with the first quenching oil KGS01 to form a first quenched mixture flow MCP01-BASE;

an asphaltene-containing stream comprising hydrocarbon components having a conventional boiling point above 530 ℃ based on the first post-quench mixture stream MCP01-BASE as a first BASE stream MCP01-CS;

a second characterizing stream MCP02, which is mixed with a second quenching oil KGS02 to form a second quenched mixture stream MCP02-BASE;

an asphaltene-containing stream comprising hydrocarbon components having conventional boiling points above 530 ℃ based on the second post-quench mixture stream MCP02-BASE as a second roadbed stream MCP02-CS;

third, after the first path of basic material flow MCP01-CS is steamed out to form a first path of vapor MCP01-CS-FV composed of low boiling point components MCP01-LCOM in a separation/fractionation part S50, a first path of reduced pressure flash evaporation base oil MCP01-S50-FL containing asphaltene-containing solid particle catalyst R10-CAT of hydrocarbon components with the conventional boiling point higher than 530 ℃ is obtained;

after separating/fractionating the portion S50, the second roadbed material flow MCP02-CS flashes off a second path of vapor MCP02-CS-FV composed of low boiling point components MCP02-LCOM, and a second path of reduced pressure flash bottom oil MCP02-S50-FL containing asphaltene-containing solid particle catalyst R10-CAT of hydrocarbon components with a conventional boiling point higher than 530 ℃;

The bottom oil is distilled in the reduced pressure flash evaporation mode to obtain part or all of the second path of reduced pressure flash evaporation bottom oil MCP02-S50-FL which is used as the bottom oil S50-FL-OUT;

fifthly, in a reduced pressure flash evaporation bottom oil circulation part, part or all of the first path of reduced pressure flash evaporation bottom oil MCP01-S50-FL is used as circulating reduced pressure flash evaporation oil MCP01-S50-FL-TOR10;

in the reaction part R10, the circulating vacuum flash oil MCP01-S50-FL-TOR10 or the intermediate hydrogenation product of the circulating vacuum flash oil MCP01-S50-FL-TOR10 is mixed and contacted with heavy oil R10F or the intermediate hydrogenation product of heavy oil R10F;

the presence or absence of a portion of the second reduced pressure flash bottoms MCP02-S50-FL is returned to the reaction section R10 for use as cycle oil MCP02-S50-FL-TOR10;

in the reaction part R10, the circulating oil MCP02-S50-FL-TOR10 or the intermediate hydrogenation product of the circulating oil MCP02-S50-FL-TOR10 is mixed and contacted with the heavy oil R10F or the intermediate hydrogenation product of the heavy oil R10F;

in the quenching oil supply part K100, the first path of quenching oil KGS01 is selected from one or more of the following streams:

in the quench oil supply section K100, the first quench oil KGS01 is a condensate oil obtained by separating the flash vapors of the first base streams MCP01-CS in the separation/fractionation section S50;

the second path of quench oil KGS02 is the condensed oil resulting from the separation of the flash vapors of the second roadbed stream MCP02-CS in the separation/fractionation section S50 in the quench oil supply section K100.

31. The method according to claim 30, wherein:

in the quench oil supply section K100, the first path of quench oil KGS01 is condensate oil obtained by flash evaporation of vapor based on the first path of base stream MCP01-CS in the separation/fractionation section S50, and is selected from one or more of the following streams:

(1) the wax oil component mainly comprises a heavy diesel component and comes from a positive pressure fractionation process based on a flash gas of a first path of base stream MCP 01-CS;

(2) mainly consists of wax oil components with conventional boiling points lower than 430 ℃ and comes from a negative pressure fractionation process based on flash evaporation vapor of a first path of base stream MCP 01-CS;

in the quench oil supply section K100, the second-circuit quench oil KGS02 is a condensate oil obtained by flash evaporation of the gas in the separation/fractionation section S50 based on the second roadbed stream MCP02-CS, selected from one or several of the following streams:

(1) a waxy oil component consisting essentially of a heavy diesel component from a positive pressure fractionation process based on flash vapors of the second roadbed stream MCP 02-CS;

(2) mainly consists of wax oil components with a conventional boiling point lower than 430 ℃ and is obtained from a negative pressure fractionation process based on flash evaporation of the MCP02-CS vapor from the second roadbed stream.

32. The method according to claim 30, wherein:

In the separation/fractionation section S50, the separation recovery system MCP02-CS-FV-SYS of the second path gas MCP02-CS-FV composed of the second path base stream MCP02-CS flash to the low boiling point component MCP02-LCOM and the separation recovery system MCP01-CS-FV of the first path gas MCP 01-CS-SYS composed of the first path base stream MCP01-CS flash to the low boiling point component MCP01-LCOM are separately or jointly arranged to share at least a part of the system.

33. The method according to claim 30, wherein:

third, in a separation/fractionation part S50, the first characteristic stream MCP01 enters a first-path first-heat low-pressure flash evaporation process and is separated into a first-path first-heat low-pressure gas and a first-path first-heat low-pressure oil; the operating pressure of the first path of first hot low-pressure flash evaporation process is greater than the atmospheric pressure;

the first path of first heat low-pressure oil is depressurized and then enters a first path of second heat low-pressure flash evaporation process to be separated into a first path of second heat low-pressure gas and a first path of second heat low-pressure oil; the operating pressure of the first path of the second hot low-pressure flash evaporation process is greater than the atmospheric pressure; the operating pressure of the first path of second hot low-pressure flash evaporation process is lower than that of the first path of first hot low-pressure flash evaporation process;

the first path of second heat low-pressure oil is separated into first path of first negative pressure flash steam and first path of first negative pressure flash oil in a first path of first negative pressure flash evaporation process;

In the separation/fractionation section S50, the second characteristic stream MCP02 enters a second first hot low pressure flash process to be separated into a second first hot low pressure gas fraction and a second first hot low pressure oil fraction; the second path first hot low pressure flash process operating pressure is greater than atmospheric pressure;

the second path of first thermal low-pressure oil is depressurized and then enters a second path of second thermal low-pressure flash evaporation process to be separated into a second path of second thermal low-pressure gas and a second path of second thermal low-pressure oil; the second path of the second hot low pressure flash process operates at a pressure greater than atmospheric pressure; the second path second hot low pressure flash process operating pressure is lower than the second path first hot low pressure flash process operating pressure;

the second path of second heat low-pressure oil is separated into a second path of first negative pressure flash steam and a second path of first negative pressure flash oil in a second path of first negative pressure flash process;

the second path of first heat low-pressure gas is separated in a first heat low-pressure gas separation and recovery system after being mixed;

the second path of second low-temperature gas is separated in a second low-temperature gas separation and recovery system after being mixed with the first path of second low-temperature gas;

the first path of first negative pressure flash steam and the second path of first negative pressure flash steam are separated in a first negative pressure flash steam separation and recovery system after being mixed.

34. The method according to claim 33, wherein:

the second path of first thermal low-pressure flash evaporation process and the first path of first thermal low-pressure flash evaporation process are carried out in different spaces isolated by partition plates in the pressure-bearing shell of the same container, and the vapor phase space of the second path of first thermal low-pressure flash evaporation process is communicated with the vapor phase space of the first path of first thermal low-pressure flash evaporation process;

the second path of second thermal low-pressure flash evaporation process and the first path of second thermal low-pressure flash evaporation process are carried out in different spaces separated by a partition plate in the pressure-bearing shell of the same container, and the vapor phase space of the second path of second thermal low-pressure flash evaporation process is communicated with the vapor phase space of the first path of second thermal low-pressure flash evaporation process;

the second path of first negative pressure flash evaporation process and the first path of first negative pressure flash evaporation process are carried out in different spaces separated by a separation plate in a shell of the same container which bears negative pressure, and the vapor phase space of the second path of first negative pressure flash evaporation process is communicated with the vapor phase space of the first path of first negative pressure flash evaporation process.

35. The method according to claim 1, wherein:

separating the base stream MCP-CS into a hot low-split gas, a hot low-split oil in a separation/fractionation section S50 in a positive pressure separation process;

Separating condensed oil obtained by the first hot low-pressure gas separation as quenching oil KGS;

the first thermal low-temperature gas is separated by using a rectifying section T11, the first thermal low-temperature gas enters the lower part of the rectifying section T11, and products are separated from the process of flowing from bottom to top along the rectifying section T11: a rectifying section T11 bottom oil, at least a portion of a stream used as the quench oil KGS, 1-way or 2-way or multi-way gas oil, overhead off-gas;

the rectifying section T11 uses the middle section to extract oil cold reflux and/or tower top cold circulation cold reflux and/or tower top cold reflux to manufacture mass transfer liquid phase;

hydrocarbon streams, with or without a waxy oil component consisting essentially of a diesel component based on cold high-fraction oil, enter the rectification section T11 for combined recovery.

36. The method according to claim 35, wherein:

the hydrocarbon stream, with or without a waxy oil component consisting essentially of a diesel component based on cold high-fraction oil, enters the rectifying section T11 at a column section position above the withdrawal of distillate oil used as quench oil KGS and below the gas oil withdrawal.

37. The method according to claim 35, wherein:

the gas oil enters a gas oil light component removing tower and is separated into bottom diesel oil of the gas oil light component removing tower and top gas of the gas oil light component removing tower;

The top gas of the gas oil light component removing tower returns to the position above the gas oil extraction port in the rectifying section T11.

38. The method according to claim 35, wherein:

2 or more paths of gas oil from the rectifying section T11 enter the same gas oil light component removing tower and are separated into bottom diesel oil of the gas oil light component removing tower and top gas of the gas oil light component removing tower;

the top gas of the gas oil light component removing tower returns to the position above the gas oil extraction port in the rectifying section T11.

39. The method according to claim 35, wherein:

the reflux tank operating pressure of the gas oil light component removal tower is 0.105-0.5 MPa (absolute pressure).

40. The method according to claim 1, wherein:

separating the base stream MCP-CS into a hot low-split gas, a hot low-split oil in a separation/fractionation section S50 in a positive pressure separation process; in the negative pressure separation process, separating the thermal low-pressure separated oil into negative pressure flash steam and negative pressure flash bottom oil;

separating condensate oil obtained by negative pressure flash steam to be used as quenching oil KGS;

the negative pressure flash steam is separated by using a negative pressure rectifying section T22, and enters the lower part of the negative pressure rectifying section T22, and products are separated in the process of flowing from bottom to top along the rectifying section T22: a rectifying section T22 bottom oil, at least a portion of the stream used as the quench oil KGS, overhead off-gas;

The rectifying section T22 uses the middle section to extract oil cold reflux and/or tower top cold circulation cold reflux and/or tower top cold reflux to manufacture mass transfer liquid phase;

hydrocarbon streams, with or without a waxy oil component consisting essentially of a diesel component based on cold high-fraction oil, enter the rectification section T22 for combined recovery.

41. The method according to claim 40, wherein:

the hydrocarbon stream, with or without a waxy oil component consisting essentially of a diesel component based on cold high-fraction oil, enters the rectifying section T22 at a column section position above the withdrawal of distillate oil used as quench oil KGS and below the gas oil withdrawal.

42. The method according to claim 40, wherein:

the gas oil enters a gas oil light component removing tower and is separated into bottom diesel oil of the gas oil light component removing tower and top gas of the gas oil light component removing tower;

the top gas of the gas oil light component removing tower returns to a position above a gas oil extraction port in the rectifying section T22.

43. The method according to claim 40, wherein:

2 or more paths of gas oil from the rectifying section T22 enter the same gas oil light component removing tower and are separated into bottom diesel oil of the gas oil light component removing tower and top gas of the gas oil light component removing tower;

The top gas of the gas oil light component removing tower returns to a position above a gas oil extraction port in the rectifying section T22.

44. The method according to claim 40, wherein:

the reflux tank operating pressure of the gas oil light component removal tower is 0.105-0.5 MPa (absolute pressure).

45. The method of claim 40 or 41 or 42 or 43 or 44, wherein:

the rectifying section T22 base oil is used for one or more of the following purposes:

(1) returning to a reaction part R10 of the heavy oil suspension bed hydro-conversion for cyclic reaction;

(2) inside the rectifying section T22, the oil enters the negative pressure flash evaporation base oil directly without passing through an oil collecting tank;

(3) and after being mixed with a part of negative pressure flash evaporation base oil, the mixture returns to a reaction part R10 of the heavy oil suspension bed hydro-conversion for cyclic reaction.

46. The method according to claim 1, wherein:

in the quenching oil supply section K100, the quenching oil KGS is hydrocarbon oil rich in aromatic hydrocarbon, and more than 80% of the quenching oil KGS is vaporized in the separation/fractionation section S50 into the flash gas of the base stream MCP-CS, so that the heat absorbed in the cooling-down stabilizing section DT10 is brought into the flash gas of the base stream MCP-CS to be utilized, and more than 80% of the gas phase component from the quenching oil KGS is released during the condensation of the flash gas of the base stream MCP-CS to complete the condensation.

47. The method according to claim 1, wherein:

in the quenching oil supply section K100, the quenching oil KGS is hydrocarbon oil rich in aromatic hydrocarbon, and more than 95% of the quenching oil KGS is vaporized in the separation/fractionation section S50 into the flash gas of the base stream MCP-CS, so that the heat absorbed in the cooling-down stabilizing section DT10 is brought into the flash gas of the base stream MCP-CS to be utilized, and more than 95% of the gas phase component from the quenching oil KGS is condensed to release heat during the condensation of the flash gas of the base stream MCP-CS.