Method for increasing naphtha yield through combined hydrocracking of wax oil heavy material and diesel oil light material

Abstract

A combined hydrocracking naphtha yield increasing method for a wax oil heavy material and a diesel oil light material is characterized in that a heavy material F1 mainly composed of wax oil components enters a first hydrocracking reaction process R21 to complete a shallow hydrocracking reaction, so that part of the wax oil components are converted into diesel oil components, and a material flow containing the diesel oil components and the wax oil components of a first hydrocracking reaction product R21P is obtained; a light material F2 mainly composed of a diesel oil component enters a second hydrocracking reaction process R22 to complete a deep hydrocracking reaction to generate a naphtha component, a second hydrocracking reaction product R22P is obtained, lean naphtha hydrocarbon oil obtained by separating R22P and / or R21P is returned to R21 and / or R22, and in order to reduce the C5-hydrocarbon yield, the naphtha yield is increased, and the C5-hydrocarbon content is reduced. According to the cracking reaction process, cyclic reaction hydrocarbon oil or external oil with the gradually decreased average carbon number is injected step by step, for example, hydrocarbon at the temperature of 200-275 DEG C is used as an R22 intermediate feed, and hydrocarbon at the temperature of 350-450 DEG C is used as an R21 intermediate feed.

Description

Technical Field

[0001] The present invention relates to a method for co - hydrocracking heavy wax oil and light diesel oil to produce more naphtha. The heavy feedstock F1 mainly composed of wax oil components enters the first hydrocracking reaction process R21 to complete a mild hydrocracking reaction, so that part of the wax oil components are converted into diesel oil components, and the first hydrocracking reaction product R21P, which is a logistics containing diesel oil components and wax oil components, and the light feedstock F2 mainly composed of diesel oil components enter the second hydrocracking reaction process R22 to complete a deep hydrocracking reaction to generate naphtha components, obtaining the second hydrocracking reaction product R22P. The naphtha - lean hydrocarbon oil obtained by separating R22P and / or R21P is returned to R21 and / or R22. In order to reduce the C 5 - hydrocarbon yield and produce more naphtha, a circulating reaction hydrocarbon oil or an external oil with a decreasing average carbon number is injected step by step according to the cracking reaction process. For example, hydrocarbons in the range of 200 - 275 °C are used as the intermediate feed for R22, and hydrocarbons in the range of 350 - 450 °C are used as the intermediate feed for R21. Background Art

[0002] C 5 - Hydrocarbons refer to the sum of hydrocarbons from C1 to C5.

[0003] The heavy feedstock F1 is mainly composed of wax oil components.

[0004] The light feedstock F2 is mainly composed of diesel oil components.

[0005] In the hydrocracking reaction process of co - producing naphtha from the heavy feedstock F1 and the light feedstock F2, the wax oil generally undergoes a series of reaction processes of "wax oil cracking into diesel oil, diesel oil cracking into naphtha, and naphtha cracking into conventional gas hydrocarbons". Therefore, when naphtha is the main product, if the light feedstock F2 and the heavy feedstock F1 start the reaction simultaneously, for the appropriate overall hydrocracking depth of the heavy feedstock F1, it will inevitably cause an over - cracking reaction for the light feedstock F2, that is, a large amount of naphtha cracking into conventional gas hydrocarbons, thus reducing the naphtha yield; conversely, when naphtha is the main product, if the light feedstock F2 and the heavy feedstock F1 start the reaction simultaneously, for the appropriate overall hydrocracking depth of the light feedstock F2, it will inevitably cause insufficient cracking depth for the heavy feedstock F1. In order to achieve the expected total cracking rate, it is necessary to increase the proportion of the circulating reaction recycle oil, that is, to increase the scale of the overall hydrocracking process, resulting in increased investment, increased energy consumption, and reduced economy of the overall hydrocracking process. Therefore, in order to reduce the C 5 - hydrocarbon yield and produce more naphtha, a reasonable feeding method is to inject a circulating reaction hydrocarbon oil or an external oil with a decreasing average carbon number step by step according to the cracking reaction process.

[0006] Generally, the organic nitrogen content of the heavy feedstock F1 and the light feedstock F2 entering the hydrocracking catalyst bed is very low, but the organic nitrogen content of the heavy feedstock F1 precursor and the light feedstock F2 precursor is usually relatively high.

[0007] The heavy feedstock F1 and the light feedstock F2 are hydrocarbon feedstocks with appropriate compositions, having relatively low organic sulfur content, organic nitrogen content, and aromatic hydrocarbon content. For example, the organic sulfur is less than 30 ppm, the organic nitrogen content is less than 30 ppm, the aromatic hydrocarbon content is less than 20% by weight, and they basically do not contain organic metal components.

[0008] Therefore, the heavy feedstock F1 and the light feedstock F2 can be distillate oils from crude oil fractionation or can be streams containing the product oil from other hydrogenation reaction processes R100, such as the reaction effluent of the hydrofining reaction process, the hot high-pressure separator oil of the reaction effluent of the hydrofining reaction process, the post-stripping hot high-pressure separator oil of the reaction effluent of the hydrofining reaction process using stripping hydrogen to remove light components, the warm high-pressure separator oil of the reaction effluent of the hydrofining reaction process, the cold high-pressure separator oil of the reaction effluent of the hydrofining reaction process, such as the reaction effluent of the pre-hydrotreatment reaction process, the hot high-pressure separator oil of the reaction effluent of the pre-hydrotreatment reaction process, the post-stripping hot high-pressure separator oil of the reaction effluent of the pre-hydrotreatment reaction process using stripping hydrogen to remove light components, the warm high-pressure separator oil of the reaction effluent of the pre-hydrotreatment reaction process, the cold high-pressure separator oil of the reaction effluent of the pre-hydrotreatment reaction process, etc.

[0009] The hydrofining reaction process refers to a hydrogenation process that mainly conducts hydrodesulfurization reaction, olefin hydrogenation saturation reaction, and aromatic hydrocarbon saturation reaction, while the proportion of hydrocracking reaction is very low. For example, the cracking rate of the associated hydrocarbon oil in the hydrofining reaction process is usually less than 5% by weight.

[0010] The hydrotreating reaction process refers to a process in which, while the hydrofining reaction process occurs, the cracking rate of the associated hydrocarbon oil is less than 10% by weight.

[0011] The hydrotreating reaction process R100 includes the hydrofining reaction process.

[0012] In the present invention, the overall combined hydrocracking process R20 includes a first hydrocracking reaction process R21 and a second hydrocracking reaction process R22.

[0013] The hydrocracking reaction conversion rate of the heavy feedstock F1 completed in the first hydrocracking reaction process R21 accounts for 20 - 65% of the overall hydrocracking reaction conversion rate of the overall combined hydrocracking process R20.

[0014] The hydrocracking reaction conversion rate of the heavy feedstock F1 completed in the second hydrocracking reaction process R22 accounts for 35 - 80% of the overall hydrocracking reaction conversion rate of the overall combined hydrocracking process R20.

[0015] Typically, when the organic nitrogen content of the heavy feedstock F1 precursor is less than 600 - 1500 ppm, at least part of the denitrification task of the heavy feedstock F1 precursor is completed through the pre-hydrotreating reaction process AR100 to be converted into the reaction effluent AR100P of the pre-hydrotreating reaction process AR100 containing the heavy feedstock F1, and the reaction effluent AR100P can usually enter the overall hydrocracking process R20.

[0016] Typically, when the organic nitrogen content of the heavy feedstock F1 is greater than 2500 ppm, at least part of the denitrification task of the heavy feedstock F1 precursor is completed through the pre-hydrotreating reaction process AR100 to be converted into the reaction effluent AR100P of the pre-hydrotreating reaction process AR100 containing the heavy feedstock F1, and preferably the hot high-pressure separated oil obtained after separating ammonia in the hot high-pressure separation process enters the overall hydrocracking process R20.

[0017] Typically, when the organic nitrogen content of the heavy feedstock F1 is between 1500 - 2500 ppm, at least part of the denitrification task of the heavy feedstock F1 precursor is completed through the pre-hydrotreating reaction process AR100 to be converted into the reaction effluent AR100P of the pre-hydrotreating reaction process AR100 containing the heavy feedstock F1. According to the operating requirements of the overall hydrocracking process R20, the reaction effluent AR100P can enter the overall hydrocracking process R20, or the hot high-pressure separated oil obtained after separating ammonia in the hot high-pressure separation process enters the overall hydrocracking process R20.

[0018] Typically, when the organic nitrogen content of the light feedstock F2 precursor is less than 600 - 1500 ppm, at least part of the denitrification task of the light feedstock F2 precursor is completed through the pre-hydrotreating reaction process BR200 to be converted into the reaction effluent BR200P of the pre-hydrotreating reaction process BR200 containing the light feedstock F2, and the reaction effluent BR200P can usually enter the overall hydrocracking process R20.

[0019] Typically, when the organic nitrogen content of the light feedstock F2 is greater than 2500 ppm, at least part of the denitrification task of the light feedstock F2 precursor is completed through the pre-hydrotreating reaction process BR200 to be converted into the reaction effluent BR200P of the pre-hydrotreating reaction process BR200 containing the light feedstock F2, and preferably the hot high-pressure separated oil obtained after separating ammonia in the hot high-pressure separation process enters the overall hydrocracking process R20.

[0020] Generally, when the organic nitrogen content of the light feedstock F2 is between 1500 and 2500 ppm, at least part of the denitrification task of the precursor of the light feedstock F2 is completed through the pre-hydrotreating reaction process BR200 to be converted into the reaction effluent BR200P of the pre-hydrotreating reaction process BR200 containing the light feedstock F2. According to the operating requirements of the overall hydrocracking process R20, the reaction effluent BR200P can enter the overall hydrocracking process R20, or the hot high-pressure separator is used to separate ammonia, and the resulting hot high-pressure oil enters the overall hydrocracking process R20.

[0021] The concept of the present invention is: a method for co-producing naphtha by the hydrocracking of a heavy gas oil feedstock and a light diesel feedstock. The heavy feedstock F1 mainly composed of gas oil components enters the first hydrocracking reaction process R21 to complete a mild hydrocracking reaction, so that part of the gas oil components are converted into diesel components, and the resulting first hydrocracking reaction product R21P is a logistics containing diesel components and gas oil components. The light feedstock F2 mainly composed of diesel components enters the second hydrocracking reaction process R22 to complete a deep hydrocracking reaction to generate naphtha components, obtaining the second hydrocracking reaction product R22P. The naphtha-lean hydrocarbon oil obtained by separating R22P and / or R21P is returned to R21 and / or R22. In order to reduce the C 5 - hydrocarbon yield and co-produce more naphtha, cyclic reaction hydrocarbon oil or external oil with a decreasing average carbon number is injected step by step according to the cracking reaction process. For example, hydrocarbons at 200-275 °C are used as the intermediate feed for R22, and hydrocarbons at 350-450 °C are used as the intermediate feed for R21.

[0022] The present invention is suitable for the process of co-producing naphtha by the hydrocracking of a heavy gas oil feedstock and a light diesel feedstock, which can significantly increase the naphtha yield and reduce the C 5 - hydrocarbon yield.

[0023] The method of the present invention has not been reported.

[0024] The method of the present invention is suitable for new plants or the renovation of existing plants.

[0025] The purpose of the invention is to provide a method for co-producing naphtha by the hydrocracking of a heavy gas oil feedstock and a light diesel feedstock. Summary of the Invention

[0026] The method for co-producing naphtha by the hydrocracking of a heavy gas oil feedstock and a light diesel feedstock of the present invention is characterized by comprising the following steps:

[0027] The overall hydrocracking reaction process R20 includes a first hydrocracking reaction process R21 and a second hydrocracking reaction process R22 that are carried out in series in the liquid phase;

[0028] The diesel component refers to a hydrocarbon component with a normal boiling point between 170 and 350 °C;

[0029] The wax oil component refers to a hydrocarbon component with a normal boiling point between 350 and 550 °C;

[0030] In the first hydrocracking reaction process R21, the heavy feed F1 mainly composed of wax oil components undergoes a mild hydrocracking reaction to convert part of the wax oil components into diesel components, obtaining the first hydrocracking reaction product R21P;

[0031] In the second hydrocracking reaction process R22, a logistics stream containing diesel components and wax oil components based on the first hydrocracking reaction product R21P undergoes a deep hydrocracking reaction to generate at least a part of the naphtha components, obtaining the second hydrocracking reaction product R22P;

[0032] The combined hydrocracking overall reaction process R20 product oil refers to a hydrocarbon oil logistics stream leaving the combined hydrocracking overall reaction process R20, which is based on the second hydrocracking reaction product R22P and / or the first hydrocracking reaction product R21P, and is a hydrocarbon oil logistics stream containing naphtha components and / or diesel components and / or wax oil components;

[0033] Separate the combined hydrocracking overall reaction process R20 product oil to obtain a hydrocarbon oil rich in naphtha components and a hydrocarbon oil KP mainly composed of diesel components and / or wax oil components with poor naphtha components;

[0034] At least a part of the logistics stream based on the hydrocarbon oil KP is used as a recycled reaction hydrocarbon oil and returns to the first hydrocracking reaction process R21 and / or the second hydrocracking reaction process R22 for cyclic reaction;

[0035] In the combined hydrocracking overall reaction process R20, according to the order of the liquid-phase series hydrocracking reaction process, the first hydrocracking reaction process R21 and the second hydrocracking reaction process R22 are divided into an upstream hydrocracking reaction process and a downstream hydrocracking reaction process;

[0036] The light feed F2 mainly composed of diesel components enters the downstream hydrocracking reaction process;

[0037] At least a part of the diesel mainly composed of hydrocarbons with a normal boiling point between 170 and 350 °C obtained by separating the combined hydrocracking overall reaction process R20 product oil does not enter the upstream hydrocracking reaction process and enters the downstream hydrocracking reaction process for cyclic reaction;

[0038] At least a part of the wax oil mainly composed of hydrocarbons with a normal boiling point between 350 and 550 °C obtained by separating the combined hydrocracking overall reaction process R20 product oil enters the upstream hydrocracking reaction process for cyclic reaction.

[0039] In the present invention, generally, during the overall reaction process R20 of combined hydrocracking, according to the cracking reaction progress, recycled reaction hydrocarbon oils or external oils with different carbon numbers are injected step by step, and the injection method is selected from one or more of the following:

[0040] ① Light diesel mainly composed of hydrocarbons with a normal boiling point of 200 - 275 °C enters the latter half of the downstream hydrocracking reaction process;

[0041] ② Heavy diesel mainly composed of hydrocarbons with a normal boiling point of 270 - 350 °C enters the initial reaction process of the downstream hydrocracking reaction process;

[0042] ③ Light wax oil mainly composed of hydrocarbons with a normal boiling point of 350 - 450 °C enters the mid - process of the upstream hydrocracking reaction process;

[0043] ④ Heavy wax oil mainly composed of hydrocarbons with a normal boiling point of 450 - 550 °C enters the initial reaction process of the upstream hydrocracking reaction process.

[0044] In the present invention, in the overall reaction process R20 of combined hydrocracking, the first hydrocracking reaction process R21 is the upstream hydrocracking reaction process, and the second hydrocracking reaction process R22 is the downstream hydrocracking reaction process. This is the forward reaction mode, and the working method is as follows:

[0045] Heavy feed F1 enters the first hydrocracking reaction process R21;

[0046] A logistics stream containing diesel components and wax oil components based on the first hydrocracking reaction product R21P enters the second hydrocracking reaction process R22, and light feed F2 enters the second hydrocracking reaction process R22 to complete the deep hydrocracking reaction to generate naphtha components and obtain the second hydrocracking reaction product R22P;

[0047] The second hydrocracking reaction product R22P is separated to obtain a hydrocarbon oil KP mainly composed of diesel components and / or wax oil components with a lean naphtha component.

[0048] In the present invention, in the overall reaction process R20 of combined hydrocracking, the first hydrocracking reaction process R21 is the downstream hydrocracking reaction process, and the second hydrocracking reaction process R22 is the upstream hydrocracking reaction process. This is the reverse reaction mode, and the working method is as follows:

[0049] In the second hydrocracking reaction process R22, wax oil mainly composed of hydrocarbons with a normal boiling point ranging from 350 to 550 °C based on the hydrocarbon oil KP enters the second hydrocracking reaction process R22 to complete the deep hydrocracking reaction to generate naphtha components and obtain the second hydrocracking reaction product R22P;

[0050] A stream containing diesel and wax oil components based on the second hydrocracking reaction product R22P enters the first hydrocracking reaction process R21, and the heavy feed F1 enters the first hydrocracking reaction process R21. The first hydrocracking reaction process R21 completes a mild hydrocracking reaction to convert part of the wax oil components into diesel components to obtain the first hydrocracking reaction product R21P;

[0051] The heavy feed F1 contains diesel components;

[0052] Separate the first hydrocracking reaction product R21P to obtain a hydrocarbon oil KP mainly composed of diesel components and / or wax oil components with a lean naphtha component.

[0053] In the present invention, when the reverse reaction mode is adopted, the heavy feed F1 contains 10-45% by weight of diesel components.

[0054] In the present invention, generally, the hydrocracking reaction conversion rate of the heavy feed F1 completed in the first hydrocracking reaction process R21 accounts for 20-65% of the total hydrocracking reaction conversion rate of the overall hydrocracking reaction process R20 of the combined hydrocracking;

[0055] The hydrocracking reaction conversion rate of the heavy feed F1 completed in the second hydrocracking reaction process R22 accounts for 35-80% of the total hydrocracking reaction conversion rate of the overall hydrocracking reaction process R20 of the combined hydrocracking;

[0056] The hydrocracking reaction conversion rate of the light feed F2 in the downstream hydrocracking reaction process is 50-85%.

[0057] In the present invention, generally, the total hydrocracking reaction naphtha yield of the heavy feed F1 in the overall hydrocracking reaction process R20 of the combined hydrocracking is 40-75%; the hydrocracking reaction naphtha yield of the light feed F2 in the downstream hydrocracking reaction process is 50-85%.

[0058] In the present invention, generally, the operating conditions of the first hydrocracking reaction process R21 are: temperature 330-450°C, pressure 8.0-20.0 MPa; the operating conditions of the second hydrocracking reaction process R22 are: temperature 330-450°C, pressure 8.0-20.0 MPa.

[0059] In the present invention, generally, the heavy feed F1 is a wax oil-containing material based on the hydrotreating reaction effluent AR100P of the hydrotreating reaction process AR100;

[0060] The method for obtaining the heavy feed F1 can be selected from one of the following:

[0061] ① The hydrotreating reaction effluent AR100P is used as the heavy feed F1;

[0062] ②The hydrotreated reaction effluent AR100P enters the hot high-pressure separation process AR100P-HS and is separated into hot high-pressure oil AR100P-HSO and hot high-pressure gas AR100P-HSV. At least a part of the hot high-pressure oil AR100P-HSO is used as the heavy feedstock F1;

[0063] ③The hydrotreated reaction effluent AR100P enters the hot high-pressure separation process AR100P-HS and is separated into hot high-pressure oil AR100P-HSO and hot high-pressure gas AR100P-HSV;

[0064] The liquid AR100P-HSOA obtained after the pressure reduction and gas removal of at least a part of the hot high-pressure oil AR100P-HSO is used as the heavy feedstock F1;

[0065] ④The hydrotreated reaction effluent AR100P enters the cold high-pressure separation process AR100P-CS and is separated into cold high-pressure oil AR100P-CSO and cold high-pressure gas AR100P-CSV. At least a part of the cold high-pressure oil AR100P-CSO is used as the heavy feedstock F1;

[0066] ⑤The hydrotreated reaction effluent AR100P is separated to obtain hydrotreated product oil AR100P-PO and hydrogen-rich gas; in the fractionation section of the hydrotreated product oil AR100P-PO, the hydrotreated product oil AR100P-PO is separated to obtain the heavy feedstock F1.

[0067] In the present invention, generally, the organic nitrogen content of the wax oil component in the feedstock hydrocarbon of the hydrotreating reaction process AR100 is selected from one of the following:

[0068] ①400 - 1500 ppm;

[0069] ②1500 - 2500 ppm;

[0070] ③Greater than 2500 ppm.

[0071] In the present invention, generally, the light feedstock F2 is a diesel-containing material based on the hydrotreated reaction effluent BR200P of the hydrotreating reaction process BR200;

[0072] The method for obtaining the light feedstock F2 can be selected from one of the following:

[0073] ①The hydrotreated reaction effluent BR200P is used as the light feedstock F2;

[0074] ②The hydrotreated reaction effluent BR200P enters the hot high-pressure separation process BR200P-HS and is separated into hot high-pressure oil BR200P-HSO and hot high-pressure gas BR200P-HSV. At least a part of the hot high-pressure oil BR200P-HSO is used as the light feedstock F2;

[0075] ③ The hydrotreating reaction effluent BR200P enters the hot high-pressure separation process BR200P-HS and is separated into hot high-pressure separated oil BR200P-HSO and hot high-pressure separated gas BR200P-HSV;

[0076] At least a part of the liquid BR200P-HSOA obtained after the hot high-pressure separated oil BR200P-HSO is depressurized and degassed is used as light material F2;

[0077] ④ The hydrotreating reaction effluent BR200P enters the cold high-pressure separation process BR200P-CS and is separated into cold high-pressure separated oil BR200P-CSO and cold high-pressure separated gas BR200P-CSV. At least a part of the cold high-pressure separated oil BR200P-CSO is used as light material F2;

[0078] ⑤ The hydrotreating reaction effluent BR200P is separated to obtain hydrotreated oil BR200P-PO and hydrogen-rich gas; in the fractionation section of the hydrotreated oil BR200P-PO, the hydrotreated oil BR200P-PO is separated to obtain light material F2.

[0079] In the present invention, generally, the organic nitrogen content of the diesel component in the feedstock hydrocarbon of the hydrotreating reaction process BR200 is selected from one of the following:

[0080] ① 400 - 1500 ppm;

[0081] ② 1500 - 2500 ppm;

[0082] ③ Greater than 2500 ppm. Specific embodiments

[0083] The normal boiling point described in the present invention refers to the vapor-liquid equilibrium temperature of a substance under one atmospheric pressure.

[0084] The normal gaseous hydrocarbon described in the present invention refers to hydrocarbons that are gaseous under normal conditions, including methane, ethane, propane, and butane.

[0085] The normal liquid hydrocarbon described in the present invention refers to hydrocarbons that are liquid under normal conditions, including pentane and hydrocarbons with higher boiling points.

[0086] The impurity elements described in the present invention refer to non-hydrogen, non-carbon, non-metallic elements such as oxygen, sulfur, nitrogen, and chlorine in the feedstock oil.

[0087] The impurity hydrogenation products described in the present invention refer to hydrogenation products of non-hydrogen and non-carbon elements in the feedstock oil, including water, hydrogen sulfide, ammonia, hydrogen chloride, etc.

[0088] The specific gravity described in the present invention, unless otherwise specified, refers to the ratio of the liquid density at normal pressure and 15.6 °C to the water density at normal pressure and 15.6 °C.

[0089] Unless otherwise specified, the composition, concentration, or content value of the components described in the present invention are all based on weight, and the weight percentage is expressed as weight %.

[0090] The diesel component described in the present invention refers to a hydrocarbon component with a normal boiling point between 170 and 350 °C.

[0091] The wax oil component described in the present invention refers to a hydrocarbon component with a normal boiling point between 350 and 550 °C.

[0092] The present invention is suitable for processing high-nitrogen inferior wax oil and can also be used for co-processing other low-nitrogen wax oils and diesel.

[0093] In the present invention, the hydrocracking method for high-nitrogen inferior wax oil generally adopts a two-stage hydrofining-hydrocracking process. The first-stage hydrogenation reaction process is a moderate hydrodenitrogenation reaction process, and the second-stage hydrogenation reaction process includes a pre-stage deep hydrodenitrogenation reaction process and a hydrocracking reaction process. A hot high-pressure separator is set between the two stages to remove nitrogen and ammonia gas from the hot high-pressure fractionator oil, and the ammonia gas enters the hot high-pressure separation gas.

[0094] Since a large amount of ammonia gas is generated after partial hydrodenitrogenation reaction in the hydrofining reaction process of high-nitrogen inferior wax oil, therefore, without excluding ammonia gas, a large amount of ammonia gas is adsorbed by the hydrofining catalyst in the subsequent hydrodenitrogenation reaction process, covering a large number of active centers of the hydrofining catalyst, which will lead to a low hydrofining reaction rate, a reduced ultimate denitrogenation rate of the hydrodenitrogenated wax oil, and an increase in the ultimate organic nitrogen content of the hydrodenitrogenated wax oil. Therefore, in order to improve the reaction rate and denitrogenation rate of the hydrogenation catalyst in the subsequent deep hydrodenitrogenation process, a primary hydrodenitrogenation-deep hydrodenitrogenation and hydrocracking method with intermediate ammonia gas removal by a two-stage method is adopted.

[0095] In the present invention, when adopting a two-stage hydrofining-hydrocracking process, the hydrofining reaction process is a moderate hydrodenitrogenation reaction process, and ammonia gas in the intermediate liquid product of the hydrodenitrogenation reaction process is removed under high-pressure conditions, so that the intermediate liquid product with ammonia gas removed enters the second-stage hydrogenation reaction process, naturally reducing the amount of ammonia gas in the deep hydrodenitrogenation process and the hydrocracking process, which is beneficial to improving the hydrodenitrogenation reaction rate and hydrocracking reaction rate in the deep hydrodenitrogenation process and the hydrocracking process.

[0096] The main advantages of the present invention are: by optimizing the average carbon number of the cracking feedstock, suppressing excessive cracking gas generation reaction, and reducing the C 5 - hydrocarbon yield, the goal of producing more naphtha is achieved.

[0097] The following details the characteristic part of the present invention.

[0098] The method for co - hydrocracking of heavy wax oil and light diesel oil to produce more naphtha of the present invention is characterized by including the following steps:

[0099] The overall co - hydrocracking reaction process R20 includes a first hydrocracking reaction process R21 and a second hydrocracking reaction process R22 that are carried out in series in the liquid phase;

[0100] The diesel component refers to a hydrocarbon component with a normal boiling point between 170 and 350 °C;

[0101] The wax oil component refers to a hydrocarbon component with a normal boiling point between 350 and 550 °C;

[0102] In the first hydrocracking reaction process R21, the heavy feedstock F1 mainly composed of wax oil components undergoes a mild hydrocracking reaction to convert part of the wax oil components into diesel components, obtaining the first hydrocracking reaction product R21P;

[0103] In the second hydrocracking reaction process R22, a logistics stream containing diesel components and wax oil components based on the first hydrocracking reaction product R21P undergoes a deep hydrocracking reaction to generate at least part of the naphtha components, obtaining the second hydrocracking reaction product R22P;

[0104] The product oil of the overall co - hydrocracking reaction process R20 refers to the hydrocarbon oil logistics leaving the overall co - hydrocracking reaction process R20 based on the second hydrocracking reaction product R22P and / or based on the first hydrocracking reaction product R21P, which is a hydrocarbon oil logistics containing naphtha components and / or diesel components and / or wax oil components;

[0105] Separate the product oil of the overall co - hydrocracking reaction process R20 to obtain a hydrocarbon oil rich in naphtha components and a hydrocarbon oil KP mainly composed of diesel components and / or wax oil components with poor naphtha components;

[0106] At least part of the logistics stream based on the hydrocarbon oil KP is used as the recycled reaction hydrocarbon oil and returned to the first hydrocracking reaction process R21 and / or the second hydrocracking reaction process R22 for cyclic reaction;

[0107] In the overall co - hydrocracking reaction process R20, according to the sequence of the liquid - phase series hydro - reaction process, the first hydrocracking reaction process R21 and the second hydrocracking reaction process R22 are divided into an upstream hydrocracking reaction process and a downstream hydrocracking reaction process;

[0108] The light feedstock F2 mainly composed of diesel components enters the downstream hydrocracking reaction process;

[0109] At least a part of the diesel oil mainly composed of hydrocarbons with a conventional boiling point between 170 and 350 °C obtained by separating the product oil of the overall hydrocracking reaction process R20 does not enter the upstream hydrocracking reaction process but enters the downstream hydrocracking reaction process for cyclic reaction;

[0110] At least a part of the wax oil mainly composed of hydrocarbons with a conventional boiling point between 350 and 550 °C obtained by separating the product oil of the overall hydrocracking reaction process R20 enters the upstream hydrocracking reaction process for cyclic reaction.

[0111] In the present invention, generally, in the overall hydrocracking reaction process R20, according to the cracking reaction progress, hydrocarbon oils for cyclic reaction or external oils with different carbon numbers are injected step by step, and the injection method is selected from one or several of the following:

[0112] ① Light diesel oil mainly composed of hydrocarbons with a conventional boiling point of 200 - 275 °C enters the latter half of the reaction process of the downstream hydrocracking reaction process;

[0113] ② Heavy diesel oil mainly composed of hydrocarbons with a conventional boiling point of 270 - 350 °C enters the starting reaction process of the downstream hydrocracking reaction process;

[0114] ③ Light wax oil mainly composed of hydrocarbons with a conventional boiling point of 350 - 450 °C enters the mid - process reaction of the upstream hydrocracking reaction process;

[0115] ④ Heavy wax oil mainly composed of hydrocarbons with a conventional boiling point of 450 - 550 °C enters the starting reaction process of the upstream hydrocracking reaction process.

[0116] In the present invention, in the overall hydrocracking reaction process R20, the first hydrocracking reaction process R21 is the upstream hydrocracking reaction process, and the second hydrocracking reaction process R22 is the downstream hydrocracking reaction process. This is the forward reaction mode, and the working method is as follows:

[0117] Heavy feedstock F1 enters the first hydrocracking reaction process R21;

[0118] The logistics containing diesel components and wax oil components based on the first hydrocracking reaction product R21P enters the second hydrocracking reaction process R22, and light feedstock F2 enters the second hydrocracking reaction process R22 to complete the deep hydrocracking reaction to generate naphtha components to obtain the second hydrocracking reaction product R22P;

[0119] The second hydrocracking reaction product R22P is separated to obtain a hydrocarbon oil KP mainly composed of diesel components and / or wax oil components with a lean naphtha component.

[0120] In the present invention, in the overall hydrocracking reaction process R20, the first hydrocracking reaction process R21 is the downstream hydrocracking reaction process, and the second hydrocracking reaction process R22 is the upstream hydrocracking reaction process. This is the reverse reaction mode, and the working method is as follows:

[0121] In the second hydrocracking reaction process R22, waxy oil mainly composed of hydrocarbons with a conventional boiling point between 350 and 550 °C based on hydrocarbon oil KP enters the second hydrocracking reaction process R22 to complete the deep hydrocracking reaction to generate naphtha components and obtain the second hydrocracking reaction product R22P;

[0122] The stream containing diesel components and waxy oil components based on the second hydrocracking reaction product R22P enters the first hydrocracking reaction process R21, and the heavy feed F1 enters the first hydrocracking reaction process R21. The first hydrocracking reaction process R21 completes the mild hydrocracking reaction to convert part of the waxy oil components into diesel components and obtain the first hydrocracking reaction product R21P;

[0123] The heavy feed F1 contains diesel components;

[0124] The first hydrocracking reaction product R21P is separated to obtain hydrocarbon oil KP mainly composed of diesel components and / or waxy oil components with a low naphtha content.

[0125] In the present invention, when the reverse reaction mode is adopted, the heavy feed F1 contains 10 - 45% by weight of diesel components.

[0126] In the present invention, generally, the hydrocracking reaction conversion rate of the heavy feed F1 completed in the first hydrocracking reaction process R21 accounts for 20 - 65% of the overall hydrocracking reaction conversion rate of the overall hydrocracking reaction process R20;

[0127] The hydrocracking reaction conversion rate of the heavy feed F1 completed in the second hydrocracking reaction process R22 accounts for 35 - 80% of the overall hydrocracking reaction conversion rate of the overall hydrocracking reaction process R20;

[0128] The hydrocracking reaction conversion rate of the light feed F2 in the downstream hydrocracking reaction process is 50 - 85%.

[0129] In the present invention, generally, the naphtha yield of the heavy feed F1 in the overall hydrocracking reaction of the overall hydrocracking reaction process R20 is 40 - 75%; the naphtha yield of the light feed F2 in the downstream hydrocracking reaction process is 50 - 85%.

[0130] In the present invention, generally, the operating conditions of the first hydrocracking reaction process R21 are as follows: temperature is 330 to 450 °C, and pressure is 8.0 to 20.0 MPa; the operating conditions of the second hydrocracking reaction process R22 are: temperature is 330 to 450 °C, and pressure is 8.0 to 20.0 MPa.

[0131] In the present invention, generally, the heavy feedstock F1 is a wax oil-containing material based on the hydrotreated reaction effluent AR100P of the hydrotreating reaction process AR100.

[0132] The method for obtaining the heavy feedstock F1 can be selected from one of the following:

[0133] ① The hydrotreated reaction effluent AR100P is used as the heavy feedstock F1.

[0134] ② The hydrotreated reaction effluent AR100P enters the hot high-pressure separation process AR100P-HS to be separated into hot high-pressure oil AR100P-HSO and hot high-pressure gas AR100P-HSV, and at least a part of the hot high-pressure oil AR100P-HSO is used as the heavy feedstock F1.

[0135] ③ The hydrotreated reaction effluent AR100P enters the hot high-pressure separation process AR100P-HS to be separated into hot high-pressure oil AR100P-HSO and hot high-pressure gas AR100P-HSV;

[0136] The liquid AR100P-HSOA obtained after at least a part of the hot high-pressure oil AR100P-HSO is depressurized and degassed is used as the heavy feedstock F1.

[0137] ④ The hydrotreated reaction effluent AR100P enters the cold high-pressure separation process AR100P-CS to be separated into cold high-pressure oil AR100P-CSO and cold high-pressure gas AR100P-CSV, and at least a part of the cold high-pressure oil AR100P-CSO is used as the heavy feedstock F1.

[0138] ⑤ The hydrotreated reaction effluent AR100P is separated to obtain hydroprocessed oil AR100P-PO and hydrogen-rich gas; in the fractionation part of the hydroprocessed oil AR100P-PO, the hydroprocessed oil AR100P-PO is separated to obtain the heavy feedstock F1.

[0139] In the present invention, generally, the organic nitrogen content of the wax oil component in the feedstock hydrocarbon of the hydrotreating reaction process AR100 is selected from one of the following:

[0140] ① 400 to 1500 ppm;

[0141] ② 1500 to 2500 ppm;

[0142] ③ Greater than 2500 ppm.

[0143] In the present invention, generally, the light material F2 is a diesel-containing material based on the hydrotreated reaction effluent BR200P of the hydrotreating reaction process BR200.

[0144] The method for obtaining the light material F2 can be selected from one of the following:

[0145] ① The hydrotreated reaction effluent BR200P is used as the light material F2.

[0146] ② The hydrotreated reaction effluent BR200P enters the hot high-pressure separation process BR200P-HS to be separated into hot high-pressure oil BR200P-HSO and hot high-pressure gas BR200P-HSV, and at least a part of the hot high-pressure oil BR200P-HSO is used as the light material F2.

[0147] ③ The hydrotreated reaction effluent BR200P enters the hot high-pressure separation process BR200P-HS to be separated into hot high-pressure oil BR200P-HSO and hot high-pressure gas BR200P-HSV;

[0148] The liquid BR200P-HSOA obtained after at least a part of the hot high-pressure oil BR200P-HSO is depressurized and degassed is used as the light material F2.

[0149] ④ The hydrotreated reaction effluent BR200P enters the cold high-pressure separation process BR200P-CS to be separated into cold high-pressure oil BR200P-CSO and cold high-pressure gas BR200P-CSV, and at least a part of the cold high-pressure oil BR200P-CSO is used as the light material F2.

[0150] ⑤ The hydrotreated reaction effluent BR200P is separated to obtain hydrogenated produced oil BR200P-PO and hydrogen-rich gas; in the fractionation part of the hydrogenated produced oil BR200P-PO, the hydrogenated produced oil BR200P-PO is separated to obtain the light material F2.

[0151] In the present invention, generally, the organic nitrogen content of the diesel component in the feedstock hydrocarbon of the hydrotreating reaction process BR200 is selected from one of the following:

[0152] ① 400 - 1500 ppm;

[0153] ② 1500 - 2500 ppm;

[0154] ③ Greater than 2500 ppm.

[0155] In the present invention, any suitable form of hydrogenation reactor can be adopted for each hydrogenation reaction process.

[0156] In the present invention, generally, a down-flow fixed-bed hydrogenation reactor is adopted for each hydrogenation reaction process.

[0157] As needed, any supplementary sulfur can be added to any hydrogenation reaction process to ensure the minimum hydrogen sulfide concentration required for the reaction process, such as 500 ppm(v) or 1000 ppm(v), so as to ensure that the hydrogen sulfide partial pressure required for the catalyst is not lower than the minimum required value. The supplementary sulfur can be a material containing hydrogen sulfide or capable of being converted into hydrogen sulfide and having no adverse effect on the hydrogenation conversion process, such as a gas or oil product containing hydrogen sulfide, or carbon disulfide, dimethyl disulfide, sulfur, etc. that generate hydrogen sulfide after contact with high-temperature hydrogen.

[0158] The general principles of the high-pressure separation process of the hydrogenation reaction effluent of the present invention are described in detail below.

[0159] The high-pressure separation process of the hydrogenation reaction effluent usually includes a cold high-pressure separator. When the hydrocarbon oil in the hydrogenation reaction effluent has a high density (such as close to the density of water), high viscosity, or is emulsified with water and difficult to separate, a hot high-pressure separator with an operating temperature usually of 150 - 450 °C is also required. At this time, the hydrogenation reaction effluent enters the hot high-pressure separator and is separated into a hot high-pressure gas mainly composed of hydrogen in volume and a hot high-pressure oil liquid mainly composed of conventional liquid hydrocarbons and possibly existing solids. After treatment, the hot high-pressure gas enters a cold high-pressure separator with an operating temperature usually of 20 - 80 °C and is separated into cold high-pressure oil and cold high-pressure gas. Since a large amount of high-boiling components enter the hot high-pressure oil liquid, the following goals are achieved: the density of the cold high-pressure oil becomes smaller, the viscosity becomes smaller, or it is easier to separate from water. The high-pressure separation process of the hydrogenation reaction effluent is provided with a hot high-pressure separator, and it also has the advantage of reducing heat loss because the hot high-pressure oil liquid can avoid the cooling process of using an air cooler or a water cooler that the hot high-pressure gas experiences. At the same time, part of the hot high-pressure 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 receiving the recycled oil, or perform recycle hydrogenation on the recycled oil. Before the hydrogenation reaction effluent or the hot high-pressure gas enters the cold high-pressure separation section, the temperature is usually reduced (generally by heat exchange with the feed of the reaction section) to about 220 - 100 °C (this temperature should be higher than the crystallization temperature of ammonium hydrosulfide in the gas phase of the hydrogenation reaction effluent), and then washing water is usually injected into it to form the hydrogenation reaction effluent after water injection. The washing water is used to absorb ammonia and other possible impurities such as hydrogen chloride, and the aqueous solution after absorbing ammonia will inevitably absorb hydrogen sulfide. In the cold high-pressure separation section, the hydrogenation reaction effluent after water injection is separated into: a cold high-pressure gas mainly composed of hydrogen in volume, a cold high-pressure oil mainly composed of conventional liquid hydrocarbons and dissolved hydrogen, and a cold high-pressure water mainly composed of water and dissolved ammonia and hydrogen sulfide. In the cold high-pressure water, the ammonia content is generally 0.5 - 15% (w), preferably 1 - 8% (w). One purpose of injecting the washing water is to absorb ammonia and hydrogen sulfide in the hydrogenation reaction effluent to prevent the formation of ammonium hydrosulfide or polysulfide ammonia crystals from clogging the heat exchanger channels and increasing the system pressure drop. The injection amount of the washing water should be determined according to the following principles: on the one hand, after the washing water is injected into the hydrogenation reaction effluent, it is divided into vapor-phase water and liquid-phase water, and the liquid-phase water volume must be greater than zero, preferably 30% or more of the total washing water; on the other hand, the washing water is used to absorb ammonia in the hydrogenation reaction effluent to prevent the ammonia concentration in the high-pressure gas from being too high and reducing the catalyst activity. Generally, the lower the ammonia volume concentration in the high-pressure gas, the better, generally not more than 200 ppm (v), preferably not more than 50 ppm (v). The operating pressure of the cold high-pressure separator is the pressure of the hydrogenation reaction section minus the actual pressure drop. The difference between the operating pressure of the cold high-pressure separation section and the hydrogenation reaction pressure should not be too low or too high, generally 0.35 - 3.2 MPa, usually 0.5 - 1.5 MPa.The hydrogen volume concentration value of the cold high-pressure separator gas should not be too low (which may lead to an increase in the operating pressure of the unit). Generally, it should not be lower than 70% (v), preferably not lower than 80% (v), and most preferably not lower than 85% (v). As mentioned above, at least a part, usually 85 - 100% of the cold high-pressure separator gas, is recycled and used in the hydrogenation reaction section to provide the necessary hydrogen volume and hydrogen concentration for the hydrogenation reaction section. To improve the investment efficiency of the unit, it is necessary to ensure that the recycled hydrogen concentration is not lower than the aforementioned lower limit value. Therefore, according to the specific feedstock properties, reaction conditions, and product distribution, a part of the cold high-pressure separator gas can be excluded to remove methane and ethane generated by the reaction. For the discharged cold high-pressure separator gas, a conventional membrane separation process, pressure swing adsorption process, or oil washing process can be used to separate hydrogen and non-hydrogen gas components, and the recovered high-concentration hydrogen is recycled and used.

[0160] When the hydrogenation unit processes high-sulfur feedstock oil, in order to reduce the hydrogen sulfide concentration in the hydrogen-rich gas of the cold high-pressure separator gas entering the hydrogenation reaction process, the hydrogen-rich gas of the cold high-pressure separator gas can be subjected to hydrogen sulfide removal treatment, and an aqueous solution containing organic amine is usually used as the hydrogen sulfide removal solvent.

[0161] Fresh hydrogen enters the hydrogenation section to supplement the hydrogen consumed in the hydrogenation reaction process. The higher the hydrogen concentration of the fresh hydrogen, the better. Generally, it should not be lower than 95% (v), and most preferably not lower than 99% (v). All the fresh hydrogen can be introduced into any hydrogenation reaction process, usually the most upstream hydrogenation reaction process in a series of hydrogenation reaction processes.

Claims

1. A method for producing more naphtha by combined hydrocracking of wax oil heavy material and diesel light material, characterized in that The following steps are involved: The combined hydrocracking overall reaction process R20 comprises a first hydrocracking reaction process R21 and a second hydrocracking reaction process R22 carried out in series in the liquid phase; The diesel component refers to a hydrocarbon component with a conventional boiling point between 170 and 350°C; The wax oil component refers to a hydrocarbon component with a conventional boiling point between 350 and 550°C; In the first hydrocracking reaction process R21, the heavy material F1 mainly composed of wax oil components undergoes a shallow hydrocracking reaction so that part of the wax oil components are converted into diesel components to obtain the first hydrocracking reaction product R21P; In the second hydrocracking reaction process R22, based on the first hydrocracking reaction product R21P containing the diesel component and the wax oil component, a deep hydrocracking reaction is performed to generate at least a portion of the naphtha component to obtain a second hydrocracking reaction product R22P; The oil produced by the combined hydrocracking overall reaction process R20 refers to a hydrocarbon oil stream based on the second hydrocracking reaction product R22P and / or based on the first hydrocracking reaction product R21P leaving the combined hydrocracking overall reaction process R20, and is a hydrocarbon oil stream containing a naphtha component and / or a diesel component and / or a wax oil component; Separating the oil produced in the combined hydrocracking overall reaction process R20 to obtain a hydrocarbon oil rich in naphtha components and obtaining a hydrocarbon oil KP poor in naphtha components and mainly composed of a diesel component and / or a wax oil component; At least a portion of the hydrocarbon oil KP-based stream is used as a circulating reaction hydrocarbon oil and returned to the first hydrocracking reaction process R21 and / or the second hydrocracking reaction process R22 for a circulating reaction; The combined hydrocracking overall reaction process R20 divides the first hydrocracking reaction process R21 and the second hydrocracking reaction process R22 into an upstream hydrocracking reaction process and a downstream hydrocracking reaction process according to the order of the liquid phase series hydrogenation reaction process; Light material F2, which mainly consists of diesel components, enters the downstream hydrocracking reaction process; At least a portion of the diesel fuel mainly composed of hydrocarbons with a conventional boiling point between 170°C and 350°C is obtained by separating the oil generated in the combined hydrocracking overall reaction process R20, and enters the downstream hydrocracking reaction process for a cyclic reaction without going through the upstream hydrocracking reaction process; At least a portion of the wax oil obtained by separating the oil generated in the combined hydrocracking overall reaction process R20, which is mainly composed of hydrocarbons with a conventional boiling point between 350 and 550° C., enters the upstream hydrocracking reaction process for a cyclic reaction.

2. The method according to claim 1, characterized in that: In the combined hydrocracking overall reaction process R20, according to the progress of the cracking reaction, the circulating reaction hydrocarbon oil or foreign oil with different carbon numbers is injected step by step, and the method is selected from one or more of the following: ① Light diesel oil, which is mainly composed of hydrocarbons with a conventional boiling point of 170-275°C, enters the second half of the downstream hydrocracking reaction process; ② The heavy diesel oil, which is mainly composed of hydrocarbons with a conventional boiling point of 270-350°C, enters the downstream hydrocracking reaction process to initiate the reaction process; ③ The half-way reaction process of the light wax oil, which is mainly composed of hydrocarbons with a conventional boiling point of 350-450°C, entering the upstream hydrocracking reaction process; ④ The initial reaction process of heavy wax oil, which is mainly composed of hydrocarbons with a conventional boiling point of 450-550°C, entering the upstream hydrocracking reaction process.

3. The method according to claim 1, characterized in that: The overall reaction process of combined hydrocracking R20, the first hydrocracking reaction process R21 is the upstream hydrocracking reaction process, and the second hydrocracking reaction process R22 is the downstream hydrocracking reaction process. This is a positive sequence reaction mode, and the working mode is: The heavy material F1 enters the first hydrocracking reaction process R21; The logistics containing diesel component and wax oil component based on the first hydrocracking reaction product R21P enters the second hydrocracking reaction process R22, and the light material F2 enters the second hydrocracking reaction process R22, completes the deep hydrocracking reaction to generate naphtha component to obtain the second hydrocracking reaction product R22P; The second hydrocracking reaction product R22P is separated to obtain a naphtha-depleted hydrocarbon oil KP mainly composed of a diesel component and / or a wax oil component.

4. The method according to claim 1, characterized in that: The overall reaction process of combined hydrocracking R20, the first hydrocracking reaction process R21 is a downstream hydrocracking reaction process, and the second hydrocracking reaction process R22 is an upstream hydrocracking reaction process. This is a reverse reaction mode, and the working mode is: In the second hydrocracking reaction process R22, the wax oil based on the hydrocarbon oil KP, which is mainly composed of hydrocarbons with a conventional boiling point between 350 and 550° C., enters the second hydrocracking reaction process R22, completes the deep hydrocracking reaction to generate a naphtha component, and obtains the second hydrocracking reaction product R22P; The logistics containing diesel component and wax oil component based on the second hydrocracking reaction product R22P enters the first hydrocracking reaction process R21, and the heavy material F1 enters the first hydrocracking reaction process R21. The first hydrocracking reaction process R21 completes the shallow hydrocracking reaction so that part of the wax oil component is converted into the diesel component to obtain the first hydrocracking reaction product R21P; The heavy material F1 contains diesel components; The first hydrocracking reaction product R21P is separated to obtain a naphtha-depleted hydrocarbon oil KP mainly composed of a diesel component and / or a wax oil component.

5. The method according to claim 4, characterized in that: The heavy material F1 contains 10 to 45% by weight of diesel components.

6. The method according to claim 1, characterized in that: The conversion rate of the hydrocracking reaction of the heavy material F1 completed in the first hydrocracking reaction process R21 accounts for 20 to 65% of the overall hydrocracking reaction conversion rate of the combined hydrocracking overall reaction process R20; The conversion rate of the hydrocracking reaction of the heavy material F1 completed in the second hydrocracking reaction process R22 accounts for 35-80% of the overall hydrocracking reaction conversion rate of the combined hydrocracking overall reaction process R20; The light material F2 has a hydrocracking reaction conversion rate of 50 to 85% in the downstream hydrocracking reaction process.

7. The method according to claim 1, characterized in that: The naphtha yield of the overall hydrocracking reaction of the heavy material F1 in the combined hydrocracking overall reaction process R20 is 40-75%; The light material F2 has a naphtha yield of 50-85% in the hydrocracking reaction of the downstream hydrocracking reaction process.

8. The method according to claim 1, characterized in that: The operating conditions of the first hydrocracking reaction process R21 are: temperature of 330-450°C and pressure of 8.0-20.0 MPa; The operating conditions of the second hydrocracking reaction process R22 are: temperature of 330-450° C. and pressure of 8.0-20.0 MPa.

9. The method according to claim 1, characterized in that: The heavy material F1 is a waxy oil-containing material based on the hydroprocessing reaction effluent AR100P of the hydroprocessing reaction process AR100.

10. The method according to claim 1, characterized in that: The heavy material F1 is a waxy oil-containing material based on the hydroprocessing reaction effluent AR100P of the hydroprocessing reaction process AR100; The method of obtaining the heavy material F1 is selected from one of the following: ① The hydroprocessing reaction effluent AR100P is used as heavy material F1; ② The hydrotreatment reaction effluent AR100P enters the hot high-pressure separation process AR100P-HS to be separated into hot high-fraction oil AR100P-HSO and hot high-fraction gas AR100P-HSV, at least a portion of the hot high-fraction oil AR100P-HSO is used as heavy material F1; ③ The hydrotreatment reaction effluent AR100P enters the hot high-pressure separation process AR100P-HS to be separated into hot high-fraction oil AR100P-HSO and hot high-fraction gas AR100P-HSV; At least a portion of the hot high-fraction oil AR100P-HSO is depressurized and degassed to obtain liquid AR100P-HSOA, which is used as heavy material F1; ④ The hydrotreatment reaction effluent AR100P enters the cold high-pressure separation process AR100P-CS to be separated into cold high-fraction oil AR100P-CSO and cold high-fraction gas AR100P-CSV, at least a portion of the cold high-fraction oil AR100P-CSO is used as heavy material F1; ⑤ Separating the hydrotreatment reaction effluent AR100P to obtain hydrogenated oil AR100P-PO and hydrogen-rich gas; in the hydrogenated oil AR100P-PO fractionation section, separating the hydrogenated oil AR100P-PO to obtain heavy material F1.

11. The method according to claim 10, characterized in that: The organic nitrogen content of the wax oil component in the feed hydrocarbon of the hydroprocessing reaction process AR100 is selected from one of the following: ①400~1500ppm; ②1500~2500ppm; ③Greater than 2500ppm.

12. The method according to claim 1, characterized in that: The light material F2 is a diesel-containing material based on the hydroprocessing reaction effluent BR200P of the hydroprocessing reaction process BR200.

13. The method according to claim 1, characterized in that: Light material F2 is a diesel-containing material based on the hydroprocessing reaction effluent BR200P of the hydroprocessing reaction process BR200; The method of obtaining the light material F2 is selected from one of the following: ① The hydroprocessing reaction effluent BR200P is used as light material F2; ② The hydrotreatment reaction effluent BR200P enters the hot high-pressure separation process BR200P-HS to be separated into hot high-fraction oil BR200P-HSO and hot high-fraction gas BR200P-HSV, at least a portion of the hot high-fraction oil BR200P-HSO is used as light material F2; ③ The hydrotreatment reaction effluent BR200P enters the hot high-pressure separation process BR200P-HS to be separated into hot high-fraction oil BR200P-HSO and hot high-fraction gas BR200P-HSV; At least a portion of the hot high-fraction oil BR200P-HSO is depressurized and degassed to obtain the liquid BR200P-HSOA, which is used as light material F2; ④ The hydrotreatment reaction effluent BR200P enters the cold high-pressure separation process BR200P-CS to be separated into cold high-fraction oil BR200P-CSO and cold high-fraction gas BR200P-CSV, at least a portion of the cold high-fraction oil BR200P-CSO is used as light material F2; ⑤ Separating the hydrotreatment reaction effluent BR200P to obtain the hydrogenated oil BR200P-PO and the hydrogen-rich gas; in the hydrogenated oil BR200P-PO fractionation section, separating the hydrogenated oil BR200P-PO to obtain the light material F2.

14. The method according to claim 13, characterized in that: The organic nitrogen content of the diesel component in the feed hydrocarbon of the hydroprocessing reaction process BR200 is selected from one of the following: ①400~1500ppm; ②1500~2500ppm; ③Greater than 2500ppm.