Systems and processes for heavy crude oil processing for maximizing aromatics production

Abstract

The present application relates to the field of heavy crude oil processing, and discloses a system and method for processing heavy crude oil to produce more aromatics. The system for processing heavy crude oil to produce more aromatics comprises a distillation unit, a residual oil hydrocracking unit, a diesel oil hydrocracking unit, a reforming unit and a non-hydro-modification unit. The system is used to process heavy crude oil, and has a high yield of aromatics.

Description

TECHNICAL FIELD

[0001] The present application relates to the field of heavy crude oil processing, in particular to a system for heavy crude oil processing for maximizing aromatics and a method for heavy crude oil processing for maximizing aromatics. BACKGROUND

[0002] At present, the processing proportion of heavy high-sulfur crude oil is gradually increasing, and the processing of heavy crude oil has become an urgent problem faced by major oil refining enterprises around the world, and the selection of a poor heavy oil processing route in a refinery is the key to affecting the economic benefits of the whole plant, especially for enterprises using heavy crude oil as raw material to achieve the goal of increasing chemical raw materials and reducing oil products, which faces certain challenges.

[0003] In the process of refinery transformation to chemical industry, a large number of oil refining and chemical technologies have rapidly developed and been applied in industry, such as heavy oil catalytic cracking technology, distillate conversion technology, aromatics production technology, and light hydrocarbon comprehensive utilization technology. These technologies make full use of the differences in the properties of different crude oil fractions and achieve the goal of "reducing oil and increasing chemicals" from different resource processing and utilization, and have become the key supporting technology for refinery transformation to chemical industry. For the overall process of a refining and chemical enterprise, the single technology advantage has a very limited impact on the overall efficiency of the plant. Only by integrating multiple single key technologies from a global perspective and optimizing the overall process of the plant can we truly achieve more efficient and more rational use of resources, achieve more optimized product structure and quality, and better support the petrochemical industry to develop towards higher quality.

[0004] CN113025378A discloses a crude oil processing method and system for maximizing olefins, which mainly processes light crude oil with an API of 35-50. According to the processing method described therein, it is difficult to process heavy crude oil with a low API, and the products mainly include low-carbon olefins, and it is difficult to eliminate finished oil. It is not suitable for refining and chemical enterprises that maximize the production of aromatic raw materials and pursue low finished oil production.

[0005] CN115678607A discloses a heavy crude oil processing method and system for maximizing chemical products, which can process heavy crude oil with an API of 10-40 to produce chemical products. According to the processing method described therein, the produced chemical products mainly include low-carbon olefins, and the yield of aromatics is less than 20%.

[0006] CN113122331A discloses a combined process and system for processing crude oil, which maximizes low-carbon olefins and does not produce aromatic products. CN108884397A discloses a method and device for converting crude oil into petrochemicals with improved product yield, which mainly produces low-carbon olefins, especially with a high ethylene yield, and the yield of aromatic products is very low, less than 20%. SUMMARY

[0007] The present application aims to overcome the problems existing in the prior art, and provides a system for processing heavy crude oil to produce more aromatics and a method for processing heavy crude oil to produce more aromatics. The system is used to process heavy crude oil, and has a high yield of aromatics.

[0008] In order to achieve the above-mentioned purpose, one aspect of the present application provides a system for processing heavy crude oil to produce more aromatics, which comprises a distillation unit, a residual oil hydrocracking unit, a diesel hydrocracking unit, a reforming unit and a non-hydro-upgrading unit.

[0009] The distillation unit is used for distilling heavy crude oil with an API degree of 20-35 to obtain straight-run liquefied gas, naphtha fraction, first distillate oil, gas oil fraction and residual oil fraction.

[0010] The residual oil hydrocracking unit is used for residual oil hydrocracking of the residual oil fraction from the distillation unit to obtain residual oil hydrocracking liquefied gas, residual oil hydrocracking naphtha, residual oil hydrocracking diesel and residual oil hydrocracking gas oil.

[0011] The diesel hydrocracking unit is used for diesel hydrocracking of the first distillate oil from the distillation unit and the residual oil hydrocracking diesel from the residual oil hydrocracking unit to obtain diesel hydrocracking liquefied gas, diesel hydrocracking light naphtha and diesel hydrocracking heavy naphtha.

[0012] The reforming unit is used for reforming of the diesel hydrocracking heavy naphtha from the diesel hydrocracking unit to obtain reforming liquefied gas, pentane oil and reforming gasoline.

[0013] The non-hydro-upgrading unit is used for non-hydro-upgrading of the diesel hydrocracking light naphtha from the diesel hydrocracking unit and the pentane oil from the reforming unit to obtain mixed aromatics.

[0014] Preferably, the system further comprises a naphtha hydrogenation unit, which is used for hydroprocessing of the light hydrocarbon recovery naphtha from the light hydrocarbon recovery unit and the residual oil hydrocracking naphtha from the residual oil hydrocracking unit to obtain naphtha hydrogenation liquefied gas, topped oil and hydrogenated heavy naphtha.

[0015] Preferably, the naphtha hydrogenation liquefied gas outlet of the naphtha hydrogenation unit is in communication with the inlet of the light hydrocarbon recovery unit.

[0016] Preferably, the topped oil outlet of the naphtha hydrogenation unit is in communication with the inlet of the non-hydro-upgrading unit.

[0017] Preferably, the hydrogenated heavy naphtha outlet of the naphtha hydrogenation unit is in communication with the inlet of the reforming unit.

[0018] Preferably, the system further comprises a wax oil hydrocracking unit for hydrocracking the wax oil fraction from the distillation unit and the residue hydrocracking wax oil from the residue hydrocracking unit to obtain a wax oil hydrocracking liquefied gas, a wax oil hydrocracking light naphtha and a wax oil hydrocracking heavy naphtha.

[0019] Preferably, the wax oil hydrocracking liquefied gas outlet of the wax oil hydrocracking unit is in communication with the inlet of the light hydrocarbon recovery unit.

[0020] Preferably, the wax oil hydrocracking light naphtha outlet of the wax oil hydrocracking unit is in communication with the inlet of the non-hydro-modification unit.

[0021] Preferably, the wax oil hydrocracking heavy naphtha outlet of the wax oil hydrocracking unit is in communication with the inlet of the reforming unit.

[0022] The second aspect of the present application provides a heavy crude oil processing method for producing more aromatics, which comprises the following steps:

[0023] (1) distilling the heavy crude oil to obtain a straight-run liquefied gas, a naphtha fraction, a first distillate oil, a wax oil fraction and a residue fraction;

[0024] (2) performing residue hydrocracking on the residue fraction obtained in step (1) to obtain a residue hydrocracking liquefied gas, a residue hydrocracking naphtha, a residue hydrocracking diesel and a residue hydrocracking wax oil;

[0025] (3) performing diesel hydrocracking on the first distillate oil obtained in step (1) and the residue hydrocracking diesel obtained in step (2) to obtain a diesel hydrocracking liquefied gas, a diesel hydrocracking light naphtha and a diesel hydrocracking heavy naphtha;

[0026] (4) performing reforming on the diesel hydrocracking heavy naphtha obtained in step (3) to obtain a reforming liquefied gas, a pentane oil and a reforming gasoline;

[0027] (5) performing non-hydro-modification on the pentane oil obtained in step (4) and the diesel hydrocracking light naphtha obtained in step (3) to obtain a mixed aromatic;

[0028] Preferably, the API degree of the heavy crude oil is 20-35.

[0029] Preferably, the method further comprises: performing hydrotreating on the light hydrocarbon recovery naphtha and the residue hydrocracking naphtha obtained in step (2) to obtain a naphtha hydroliquefied gas, a topped oil, a hydrotreated heavy naphtha; then performing light hydrocarbon recovery treatment on the naphtha hydroliquefied gas, non-hydro-modification on the topped oil and reforming on the hydrotreated heavy naphtha.

[0030] Preferably, the method further comprises: subjecting the wax oil fraction obtained in step (1) and the residue hydrocracking wax oil obtained in step (2) to wax oil hydrocracking to obtain wax oil hydrocracking liquefied gas, wax oil hydrocracking light naphtha and wax oil hydrocracking heavy naphtha; then subjecting the wax oil hydrocracking liquefied gas to light hydrocarbon recovery treatment, the wax oil hydrocracking light naphtha to non-hydro modification, and the wax oil hydrocracking heavy naphtha to reforming.

[0031] By the above technical solution, the beneficial effects of the present application include:

[0032] The system for processing heavy crude oil to produce more aromatics provided by the present application uses heavy crude oil with low API as raw material, integrates multiple processing units, and uses the product processed by one unit as the raw material of another unit, which can fully combine the properties of the product components in different units, is beneficial to improve the overall efficiency of the process and the yield of aromatics, improves the resource utilization efficiency, and can meet the demand of refining enterprises that maximize the production of aromatics raw materials. BRIEF DESCRIPTION OF DRAWINGS

[0033] Figure 1 is a schematic diagram of the system for processing heavy crude oil to produce more aromatics provided by the present application;

[0034] Figure 2 is a schematic diagram of the refinery heavy crude oil processing process provided by Comparative Example 1.

[0035] REFERENCE NUMERALS

[0036] In Figure 1 ,

[0037] 1, heavy crude oil; 2, distillation unit; 3, light hydrocarbon recovery unit; 4, naphtha hydrogenation unit; 5, reforming unit; 6, diesel hydrocracking unit; 7, wax oil hydrocracking unit; 8, residual oil hydrocracking unit; 9, non-hydro-upgrading unit; 10, aromatic complex unit; 11, hydrogen production unit; 12, hydrogen production feedstock; 13, hydrogen; 14, straight-run liquefied petroleum gas; 15, naphtha fraction; 16, first distillate oil; 17, wax oil fraction; 18, residual oil fraction; 19, light hydrocarbon recovery naphtha; 20, light hydrocarbon recovery liquefied petroleum gas; 21, naphtha hydrogenation liquefied petroleum gas; 22, top oil; 23, hydrogenated heavy naphtha; 24, reforming liquefied petroleum gas; 25, pentane oil; 26, reforming gasoline; 27, diesel hydrocracking liquefied petroleum gas; 28, diesel hydrocracking light naphtha; 29, diesel hydrocracking heavy naphtha; 30, wax oil hydrocracking liquefied petroleum gas; 31, wax oil hydrocracking light naphtha; 32, wax oil hydrocracking heavy naphtha; 33, residual oil hydrocracking liquefied petroleum gas; 34, residual oil hydrocracking naphtha; 35, residual oil hydrocracking diesel; 36, residual oil hydrocracking wax oil; 37, mixed aromatic hydrocarbon; 38, aromatic raffinate; 39, benzene; 40, xylene; 41, C9+ aromatic hydrocarbon.

[0038] In Figure 2 ,

[0039] 42, heavy crude oil; 43, atmospheric and vacuum distillation unit; 44, light hydrocarbon recovery unit; 45, naphtha hydrogenation unit; 46, reforming unit; 47, diesel hydrocracking unit; 48, aviation fuel hydrogenation unit; 49, wax oil hydrocracking unit; 50, delayed coking unit; 51, isomerization unit; 52, hydrogen production unit; 53, aromatic complex unit; 54, liquefied petroleum gas; 55, naphtha; 56, aviation fuel fraction; 57, diesel; 58, wax oil; 59, heavy oil; 60, light hydrocarbon recovery liquefied petroleum gas; 61, light hydrocarbon recovery naphtha; 62, naphtha hydrogenation liquefied petroleum gas; 63, top oil; 64, hydrogenated heavy naphtha; 65, reforming liquefied petroleum gas; 66, pentane oil; 67, reforming gasoline; 68, hydrogenated aviation fuel; 69, aromatic raffinate; 70, diesel hydrocracking liquefied petroleum gas; 71, diesel hydrocracking light naphtha; 72, diesel hydrocracking heavy naphtha; 73, hydrocracking aviation fuel; 74, isomerized gasoline; 75, wax oil hydrocracking liquefied petroleum gas; 76, wax oil hydrocracking light naphtha; 77, wax oil hydrocracking heavy naphtha; 78, wax oil hydrocracking aviation fuel; 79, diesel; 80, coking naphtha; 81, coking diesel; 82, coking wax oil; 83, hydrogen production feedstock; 84, hydrogen; 85, benzene; 86, xylene; 87, C9+ aromatic hydrocarbon; 88, aviation fuel; 89, gasoline; 90, petroleum coke. DETAILED DESCRIPTION

[0040] The endpoints of the ranges and any values disclosed herein are not limited to the precise values recited as the exact dimensions are not critical to the invention. Each integer value within the range is also contemplated. The endpoints of the ranges and any value between the recited values should be considered as alternatives as the exact dimensions are not critical to the invention. For values which are less than one, one unit is considered to be 0.0001, 0.001, 0.01 or 0.1 as appropriate. For values which are greater than one, one unit is considered to be 1, 10, 100, 1,000 or 10,000 as appropriate. These are only examples of what is specifically

[0041] The present application provides a system for processing heavy crude oil to produce aromatics, the system comprising: a distillation unit 2, a residue hydrocracking unit 8, a diesel hydrocracking unit 6, a reforming unit 5 and a non-hydro-upgrading unit 9.

[0042] The distillation unit 2 is used for distilling heavy crude oil with API degree of 20-35 to obtain straight-run liquefied gas, naphtha fraction, first distillate oil, gas oil fraction and residue fraction.

[0043] The residue hydrocracking unit 8 is used for residue hydrocracking the residue fraction from the distillation unit 2 to obtain residue hydrocracking liquefied gas, residue hydrocracking naphtha, residue hydrocracking diesel and residue hydrocracking gas oil.

[0044] The diesel hydrocracking unit 6 is used for diesel hydrocracking the first distillate oil from the distillation unit 2 and the residue hydrocracking diesel from the residue hydrocracking unit 8 to obtain diesel hydrocracking liquefied gas, diesel hydrocracking light naphtha and diesel hydrocracking heavy naphtha.

[0045] The reforming unit 5 is used for reforming the diesel hydrocracking heavy naphtha from the diesel hydrocracking unit 6 to obtain reforming liquefied gas, pentane oil and reforming gasoline.

[0046] The non-hydro-upgrading unit 9 is used for non-hydro-upgrading the diesel hydrocracking light naphtha from the diesel hydrocracking unit 6 and the pentane oil from the reforming unit 5 to obtain mixed aromatics.

[0047] In the present application, the first distillate oil refers to kerosene fraction and diesel fraction.

[0048] In the present application, the terms "crude oil", "liquefied gas", "naphtha", "gas oil", "diesel", "kerosene", "residue", "pentane oil", "gasoline" and the like have the definitions well known to those skilled in the art.

[0049] The present application uses heavy crude oil with low API as raw material, integrates a series of oil refining processes, synchronously solves the efficient processing problem of light components and heavy components of heavy crude oil, aims to produce aromatics, greatly improves the yield of aromatic products, and does not produce finished oil, thereby providing a new scheme for oil conversion of a refinery.

[0050] In the present application, API is a measure of the density of petroleum and petroleum products, which is formulated by American Petroleum Institute. The greater the value, the lighter the crude oil; the smaller the value, the heavier the crude oil, which is more difficult to handle.

[0051] The system of the present application can be used to treat heavy crude oil. In the present application, the API of the heavy crude oil is 20-35, preferably 25-32. For example, it can be 20, 21, 22, 23, 24, 25, 26, 27, 28, 29, 30, 31, 32, 33, 34, 35, and any value in the range formed by any two of these values.

[0052] According to the present application, preferably, the sulfur content of the heavy crude oil is 0.01-3wt%.

[0053] The system of the present application does not have a particular limitation on the type of heavy crude oil to be treated, and can be any heavy crude oil commonly used in the art.

[0054] The distillation unit 2 of the present application can be a conventional selection in the art. Preferably, the distillation unit 2 is a conventional distillation unit.

[0055] The present application does not have a particular limitation on the device used in the conventional distillation unit, and can be a conventional selection in the art, as long as it can achieve its function (obtain a specific material).

[0056] The present application does not have a particular limitation on the device used in the residue hydrocracking unit 8, the diesel hydrocracking unit 6, the reforming unit 5 and the non-hydro-upgrading unit 9, and can be a conventional selection in the art, as long as it can achieve its respective function.

[0057] In the present application, the residue hydrocracking unit 8 can be a slurry bed residue hydrocracking unit or a boiling bed residue hydrocracking unit.

[0058] In the present application, the naphtha fraction obtained by distillation in the distillation unit 2 can contain part of the straight-run liquefied gas, the straight-run liquefied gas can contain part of the naphtha fraction, and the different liquefied gas obtained by other units can contain part of the light gasoline fraction, which needs to be further separated. Preferably, the system further comprises a light hydrocarbon recovery unit 3, which is used for light hydrocarbon recovery treatment of the straight-run liquefied gas and the naphtha fraction from the distillation unit 2, the residue hydrocracking liquefied gas from the residue hydrocracking unit 8, the diesel hydrocracking liquefied gas from the diesel hydrocracking unit 6, and the reforming liquefied gas from the reforming unit 5, to obtain light hydrocarbon recovery liquefied gas and light hydrocarbon recovery naphtha.

[0059] Preferably, the light hydrocarbon recovery liquefied gas outlet of the light hydrocarbon recovery unit 3 is communicated with the inlet of the non-hydrogen modification unit 9. With this preferred embodiment, the light hydrocarbon recovery liquefied gas is sent to the non-hydrogen modification unit 9 for non-hydrogen modification.

[0060] The present application does not have special limitations on the device used by the light hydrocarbon recovery unit 3, which can be a conventional choice in the art as long as it can achieve its function.

[0061] According to the present application, preferably, the system further comprises a naphtha hydrogenation unit 4 for hydrogenating the light hydrocarbon recovery naphtha from the light hydrocarbon recovery unit 3 and the residue hydrocracking naphtha from the residue hydrocracking unit 8 to obtain naphtha hydrogenation liquefied gas, topped oil, and hydrogenated heavy naphtha.

[0062] According to the present application, preferably, the naphtha hydrogenation liquefied gas outlet of the naphtha hydrogenation unit 4 is communicated with the inlet of the light hydrocarbon recovery unit 3.

[0063] According to the present application, preferably, the topped oil outlet of the naphtha hydrogenation unit 4 is communicated with the inlet of the non-hydrogen modification unit 9.

[0064] According to the present application, preferably, the hydrogenated heavy naphtha outlet of the naphtha hydrogenation unit 4 is communicated with the inlet of the reforming unit 5.

[0065] In the above preferred embodiment, the naphtha hydrogenation liquefied gas is sent to the light hydrocarbon recovery unit 3 for light hydrocarbon recovery treatment, the topped oil is sent to the non-hydrogen modification unit 9 for non-hydrogen modification, and the hydrogenated heavy naphtha is sent to the reforming unit 5 for reforming, which is conducive to further improving the yield of aromatics.

[0066] The present application does not have special limitations on the device used by the naphtha hydrogenation unit 4, which can be a conventional choice in the art as long as it can achieve the above functions.

[0067] According to the present application, preferably, the system further comprises a wax oil hydrocracking unit 7 for hydrocracking the wax oil fraction from the distillation unit 2 and the residue hydrocracking wax oil from the residue hydrocracking unit 8 to obtain wax oil hydrocracking liquefied gas, wax oil hydrocracking light naphtha, and wax oil hydrocracking heavy naphtha.

[0068] According to the present application, preferably, the wax oil hydrocracking liquefied gas outlet of the wax oil hydrocracking unit 7 is communicated with the inlet of the light hydrocarbon recovery unit 3.

[0069] According to the present application, preferably, the wax oil hydrocracking light naphtha outlet of the wax oil hydrocracking unit 7 is communicated with the inlet of the non-hydrogen modification unit 9.

[0070] According to the present application, preferably, the wax oil hydrocracking heavy naphtha outlet of the wax oil hydrocracking unit 7 is communicated with the inlet of the reforming unit 5.

[0071] In the above preferred embodiment, the wax oil hydrocracking liquefied gas is sent into the light hydrocarbon recovery unit 3 for light hydrocarbon recovery treatment, the wax oil hydrocracking light naphtha is sent into the non-hydro modification unit 9 for non-hydro modification, and the wax oil hydrocracking heavy naphtha is sent into the reforming unit 5 for reforming, which is conducive to further improving the yield of aromatic hydrocarbons.

[0072] The device used by the wax oil hydrocracking unit 7 in the present application is not particularly limited and can be a conventional selection in the art as long as the above functions can be achieved.

[0073] According to the present application, preferably, the system further comprises an aromatic hydrocarbon combination unit 10 for processing the reforming gasoline from the reforming unit 5 and the mixed aromatic hydrocarbons from the non-hydro modification unit 9 to obtain aromatic hydrocarbon products and aromatic hydrocarbon raffinate.

[0074] Preferably, the aromatic hydrocarbon raffinate outlet of the aromatic hydrocarbon combination unit 10 is communicated with the inlet of the non-hydro modification unit 9. With this preferred embodiment, the aromatic hydrocarbon raffinate is sent into the non-hydro modification unit 9 for non-hydro modification.

[0075] The device used by the aromatic hydrocarbon combination unit 10 in the present application is not particularly limited and can be a conventional selection in the art as long as the above functions can be achieved. For example, the aromatic hydrocarbon combination unit 10 can include one or more of an aromatic hydrocarbon extraction device, a disproportionation-isomerization device, and a C8 separation device.

[0076] According to the present application, preferably, the aromatic hydrocarbon products include at least one of benzene, toluene, and xylene. The above substances are typical high-value aromatic hydrocarbons in the art, and the aromatic hydrocarbon products generated by the present application are mainly composed of the above high-value aromatic hydrocarbons.

[0077] In the present application, the hydrogen required by the residue hydrocracking unit 8, the diesel hydrocracking unit 6, the naphtha hydrocracking unit 4, and the wax oil hydrocracking unit 7 can be provided externally or by self-production. Preferably, the system further comprises a hydrogen production unit 11 for processing hydrogen production raw material 12 to obtain hydrogen 13.

[0078] According to a specific embodiment of the present application, as shown in Figure 1 The heavy crude oil 1 is sent into the distillation unit 2 for distillation to obtain straight-run liquefied gas 14, naphtha fraction 15, first distillate oil 16, wax oil fraction 17, and residue fraction 18;

[0079] The residue fraction 18 from the distillation unit 2 is subjected to residue hydrocracking in a residue hydrocracking unit 8 to obtain a residue hydrocracking liquefied gas 33, a residue hydrocracking naphtha 34, a residue hydrocracking diesel 35, and a residue hydrocracking gas oil 36; the first distillate oil 16 from the distillation unit 2 and the residue hydrocracking naphtha 35 from the residue hydrocracking unit 8 are subjected to diesel hydrocracking in a diesel hydrocracking unit 6 to obtain a diesel hydrocracking liquefied gas 27, a diesel hydrocracking light naphtha 28, and a diesel hydrocracking heavy naphtha 29;

[0080] The light hydrocarbon recovery naphtha 19 from the light hydrocarbon recovery unit 3 described below, the residue hydrocracking naphtha 34 from the residue hydrocracking unit 8 are subjected to hydrotreatment in a naphtha hydrogenation unit 4 to obtain a naphtha hydrogenation liquefied gas 21, a topped oil 22, a hydrogenated heavy naphtha 23;

[0081] The gas oil fraction 17 from the distillation unit 2 and the residue hydrocracking gas oil 36 from the residue hydrocracking unit 8 are subjected to gas oil hydrocracking in a gas oil hydrocracking unit 7 to obtain a gas oil hydrocracking liquefied gas 30, a gas oil hydrocracking light naphtha 31, and a gas oil hydrocracking heavy naphtha 32;

[0082] The diesel hydrocracking heavy naphtha 29 from the diesel hydrocracking unit 6, the gas oil hydrocracking heavy naphtha 32 from the gas oil hydrocracking unit 7, the hydrogenated heavy naphtha 23 from the naphtha hydrogenation unit 4 are subjected to reforming in a reforming unit 5 to obtain a reforming liquefied gas 24, a pentane oil 25, and a reforming gasoline 26;

[0083] The straight-run liquefied gas 14 and the naphtha fraction 15 from the distillation unit 2, the naphtha hydrogenation liquefied gas 21 from the naphtha hydrogenation unit 4, the diesel hydrocracking liquefied gas 27 from the diesel hydrocracking unit 6, the gas oil hydrocracking liquefied gas from the gas oil hydrocracking unit 7, the residue hydrocracking liquefied gas 33 from the residue hydrocracking unit 8, the reforming liquefied gas 24 from the reforming unit 5 are subjected to light hydrocarbon recovery treatment in a light hydrocarbon recovery unit 3 to obtain a light hydrocarbon recovery liquefied gas 20 and a light hydrocarbon recovery naphtha 19;

[0084] The light hydrocarbon recovery liquefied gas 20 from the light hydrocarbon recovery unit 3, the topped oil 22 from the naphtha hydrogenation unit 4, the pentane oil 25 from the reforming unit 5, the diesel hydrocracking light naphtha 28 from the diesel hydrocracking unit 6, the gas oil hydrocracking light naphtha 31 from the gas oil hydrocracking unit 7, the aromatic raffinate 38 from the aromatic complex unit 10 described below are subjected to non-hydrogen reforming in a non-hydrogen reforming unit 9 to obtain a mixed aromatic hydrocarbon 37;

[0085] Reformed gasoline 26 from reforming unit 5 and mixed aromatics 37 from non-hydrogen-reforming unit 9 are fed into aromatics complex unit 10 for processing to obtain aromatic products (benzene 39, xylene 40, C9+ aromatics 41) and aromatics raffinate 38.

[0086] The hydrogen required by the residue hydrocracking unit 8, diesel hydrocracking unit 6, naphtha hydrocracking unit 4, and wax oil hydrocracking unit 7 is provided by hydrogen 13 produced from hydrogen feedstock 12 introduced into the hydrogen production unit 11. Figure 1 (Not fully displayed in the image).

[0087] It should be noted that the residue hydrocracking naphtha 34 flowing out from residue hydrocracking unit 8 is... Figure 1 Since it is inconvenient to directly link to naphtha hydrogenation unit 4, 34 is additionally introduced from naphtha hydrogenation unit 4. These two materials 34 represent the same material.

[0088] A second aspect of the present invention provides a method for processing heavy crude oil that yields abundant aromatics, the method comprising the following steps:

[0089] (1) Distill heavy crude oil to obtain straight-run liquefied gas, naphtha fraction, first fraction oil, wax oil fraction and residue oil fraction;

[0090] (2) The residue fraction obtained in step (1) is subjected to residue hydrocracking to obtain residue hydrocracking liquefied petroleum gas, residue hydrocracking naphtha, residue hydrocracking diesel oil and residue hydrocracking wax oil.

[0091] (3) The first distillate oil obtained in step (1) and the residue hydrocracking diesel obtained in step (2) are subjected to diesel hydrocracking to obtain diesel hydrocracking liquefied petroleum gas, diesel hydrocracking light naphtha and diesel hydrocracking heavy naphtha.

[0092] (4) The diesel hydrocracking heavy naphtha obtained in step (3) is reformed to obtain reformed liquefied petroleum gas, pentane oil and reformed gasoline.

[0093] (5) The pentane oil obtained in step (4) and the light naphtha from diesel hydrocracking obtained in step (3) are subjected to non-hydrogenation reforming to obtain mixed aromatics;

[0094] The API gravity of the heavy crude oil is 20-35.

[0095] In this invention, the API gravity of the heavy crude oil is 20-35, preferably 25-32. For example, it can be 20, 21, 22, 23, 24, 25, 26, 27, 28, 29, 30, 31, 32, 33, 34, 35, or any value within the range formed by any two of these values.

[0096] According to the present application, preferably, the sulfur content of the heavy crude oil is 0.01-3wt%.

[0097] The distillation in step (1) can be a conventional selection in the art. Preferably, the distillation in step (1) is a conventional atmospheric and vacuum distillation.

[0098] The present application does not have specific limitations on the specific operating conditions of the distillation in step (1), as long as the above-mentioned straight-run liquefied petroleum gas, naphtha fraction, first distillate oil, wax oil fraction and residual oil fraction products can be obtained, and conventional methods in the art can be referred to.

[0099] The conditions for the residual oil hydrocracking in the present application can be a conventional selection in the art. Preferably, the conditions for the residual oil hydrocracking in step (2) include: a reaction temperature of 380-470℃, a pressure of 10-25MPa, a volume space velocity of 0.05-2h -1 .

[0100] Preferably, the residual oil hydrocracking is carried out under the action of a residual oil hydrocracking catalyst.

[0101] The residual oil hydrocracking catalyst in the present application can be a conventional selection in the art, and the present application does not have specific limitations thereon.

[0102] Preferably, the method further comprises: separating the residual oil hydrocracking product to obtain a residual oil hydrocracking liquefied petroleum gas, a residual oil hydrocracking naphtha, a residual oil hydrocracking diesel oil and a residual oil hydrocracking wax oil.

[0103] The present application does not have specific limitations on the specific method of separation, and methods in the art can be referred to.

[0104] In the present application, in the following processes of diesel oil hydrocracking, reforming, hydroprocessing, wax oil hydrocracking, the products also need to be separated to obtain each material. The separation is carried out with reference to the methods in the art.

[0105] The conditions for the diesel oil hydrocracking in the present application can be a conventional selection in the art. Preferably, the conditions for the diesel oil hydrocracking in step (3) include: a reaction temperature of 300-420℃, a pressure of 4-13MPa, a volume space velocity of 0.2-5h -1 .

[0106] Preferably, the diesel oil hydrocracking is carried out under the action of a diesel oil hydrocracking catalyst.

[0107] The diesel oil hydrocracking catalyst in the present application can be a conventional selection in the art, and the present application does not have specific limitations thereon.

[0108] The reforming conditions according to the present application can be conventional selection in the art. Preferably, the reforming conditions in step (4) include: reaction temperature is 460-540℃, pressure is 0.3-2MPa, mass space velocity is 0.5-4h -1 .

[0109] Preferably, the reforming is carried out in the presence of a reforming catalyst.

[0110] The reforming catalyst according to the present application can be conventional selection in the art, and the present application has no particular limitation thereon.

[0111] The non-hydrogen modification conditions according to the present application can be conventional selection in the art. Preferably, the non-hydrogen modification conditions in step (5) include: reaction temperature is 300-600℃, pressure is 0.1-1MPa, mass space velocity is 0.3-1h -1 .

[0112] Preferably, the non-hydrogen modification is carried out in the presence of a non-hydrogen modification catalyst.

[0113] The non-hydrogen modification catalyst according to the present application can be conventional selection in the art, and the present application has no particular limitation thereon.

[0114] According to the present application, preferably, the method further comprises: subjecting the straight-run liquefied gas and naphtha fraction obtained in step (1), the residue hydrocracking liquefied gas obtained in step (2), the diesel hydrocracking liquefied gas obtained in step (3), and the reforming liquefied gas obtained in step (4) to light hydrocarbon recovery treatment to obtain light hydrocarbon recovery liquefied gas and light hydrocarbon recovery naphtha; and then subjecting the light hydrocarbon recovery liquefied gas to non-hydrogen modification.

[0115] According to the present application, preferably, the method further comprises: subjecting the light hydrocarbon recovery naphtha and the residue hydrocracking naphtha obtained in step (2) to hydrogen treatment to obtain naphtha hydrogenation liquefied gas, topped oil, and hydrogenated heavy naphtha; and then subjecting the naphtha hydrogenation liquefied gas to light hydrocarbon recovery treatment, the topped oil to non-hydrogen modification, and the hydrogenated heavy naphtha to reforming.

[0116] According to the present application, preferably, the hydrogen treatment conditions include: reaction temperature is 200-320℃, pressure is 0.5-4MPa, volume space velocity is 1-15h -1 .

[0117] Preferably, the hydrogen treatment is carried out in the presence of a naphtha hydrogenation catalyst.

[0118] The naphtha hydrogenation catalyst according to the present application can be conventional selection in the art, and the present application has no particular limitation thereon.

[0119] According to the present application, preferably, the method further comprises: subjecting the wax oil fraction obtained in step (1) and the residue hydrocracking wax oil obtained in step (2) to wax oil hydrocracking to obtain wax oil hydrocracking liquefied gas, wax oil hydrocracking light naphtha and wax oil hydrocracking heavy naphtha; then subjecting the wax oil hydrocracking liquefied gas to light hydrocarbon recovery treatment, the wax oil hydrocracking light naphtha to non-hydro modification, and the wax oil hydrocracking heavy naphtha to reforming.

[0120] The conditions for the wax oil hydrocracking according to the present application can be conventionally selected in the art. Preferably, the conditions for the wax oil hydrocracking include: a reaction temperature of 320-430℃, a pressure of 8-18 MPa, a volume space velocity of 0.1-3h -1 .

[0121] Preferably, the wax oil hydrocracking is carried out in the presence of a wax oil hydrocracking catalyst.

[0122] The wax oil hydrocracking catalyst according to the present application can be conventionally selected in the art, and the present application does not have a particular limitation thereon.

[0123] According to the present application, preferably, the method further comprises: processing the reforming gasoline obtained in step (4) and the mixed aromatic hydrocarbon obtained in step (5) to obtain an aromatic hydrocarbon product and an aromatic hydrocarbon raffinate; and then subjecting the aromatic hydrocarbon raffinate to non-hydro modification.

[0124] Preferably, according to the present application, preferably, the aromatic hydrocarbon product comprises at least one of benzene, toluene and xylene.

[0125] In the present application, the hydrogen required in the residue hydrocracking, the diesel hydrocracking, the naphtha hydrotreating and the wax oil hydrocracking can be provided externally or by self-production. The present application preferably adopts self-production.

[0126] The present application will be described in detail below through examples.

[0127] Example 1

[0128] According to the procedure shown in the following scheme. Figure 1

[0129] A heavy crude oil 1 with API of 30.6 and sulfur content of 2.6wt% was fed into a distillation unit 2 (a conventional distillation unit) for distillation to separate out straight-run liquefied gas 14, naphtha fraction 15 (boiling range 40-170℃), first distillate oil 16 (boiling range 170-350℃), wax oil fraction 17 (boiling range 350-510℃), and residue fraction 18 (initial boiling point >510℃). The straight-run liquefied gas 14 and the naphtha fraction 15 were subjected to light hydrocarbon recovery treatment by a light hydrocarbon recovery unit 3 to separate out light hydrocarbon recovery liquefied gas 20 and light hydrocarbon recovery naphtha 19.​

[0130] The residue fraction 18 is subjected to residue hydrocracking in a residue hydrocracking unit 8 (slurry bed residue hydrocracking unit) to obtain a residue hydrocracking liquefied gas 33, a residue hydrocracking naphtha 34 (distillation range 35-180℃), a residue hydrocracking diesel 35 (distillation range 180-350℃) and a residue hydrocracking gas oil 36 (distillation range 350-500℃); the conditions of residue hydrocracking include: reaction temperature 425℃, reaction pressure 15 MPa, volume space velocity 0.6h -1 ; the residue hydrocracking catalyst is a molybdenum naphthenate.

[0131] The light hydrocarbon recovery naphtha 19 and the residue hydrocracking naphtha 34 are subjected to hydrotreating in a naphtha hydrocracking unit 4 to obtain a naphtha hydrocracking liquefied gas 21, a front-end oil 22 (final boiling point <60℃) and a hydrocracking heavy naphtha 23 (distillation range 60-180℃); the conditions of naphtha hydrocracking include: reaction temperature 290℃, reaction pressure 2 MPa, volume space velocity 6h -1 ; the naphtha hydrocracking catalyst is a RS-40 catalyst developed by Petrochemical Research Institute.

[0132] The gas oil fraction 17 and the residue hydrocracking gas oil 36 are subjected to gas oil hydrocracking in a gas oil hydrocracking unit 7 to obtain a gas oil hydrocracking liquefied gas 30, a gas oil hydrocracking light naphtha 31 (distillation range 34-65℃) and a gas oil hydrocracking heavy naphtha 32 (distillation range 65-175℃); the conditions of gas oil hydrocracking include: reaction temperature 380℃, pressure 15 MPa, volume space velocity 0.5h -1 ; the gas oil hydrocracking catalyst is a RHC-210 catalyst developed by Petrochemical Research Institute.

[0133] The first distillate oil 16 and the residue hydrocracking diesel 35 are subjected to diesel hydrocracking in a diesel hydrocracking unit 6 to obtain a diesel hydrocracking liquefied gas 27, a diesel hydrocracking light naphtha 28 (distillation range 34-65℃) and a diesel hydrocracking heavy naphtha 29 (distillation range 65-175℃); the conditions of diesel hydrocracking include: reaction temperature 375℃, pressure 12 MPa, volume space velocity 1h -1 ; the diesel hydrocracking catalyst is a RHC-210F catalyst developed by Petrochemical Research Institute.

[0134] The hydrocracking heavy naphtha 23, the gas oil hydrocracking heavy naphtha 32 and the diesel hydrocracking heavy naphtha 29 are subjected to reforming in a reforming unit 5 to obtain a reforming liquefied gas 24, a pentane oil 25 (final boiling point <60℃) and a reforming gasoline 26 (distillation range 60-180℃); the conditions of reforming include: reaction temperature 520℃, pressure 0.35 MPa, mass space velocity 2h-1 ; the reforming catalyst is PS-VI catalyst developed by Research Institute of Petroleum Processing.

[0135] The light hydrocarbon recovery liquefied gas 20, the wax oil hydrocracking light naphtha 31, the diesel hydrocracking light naphtha 28, the topped oil 22, the pentane oil 25 and the aromatic raffinate 38 obtained below are subjected to non-hydro upgrading by the non-hydro upgrading unit 9 to obtain mixed aromatics 37; the non-hydro upgrading conditions include that the reaction temperature is 530°C, the pressure is 0.2 MPa, the mass space velocity is 0.6 h -1 -1, and the non-hydro upgrading catalyst is RF-4 light hydrocarbon aromatization catalyst developed by Research Institute of Petroleum Processing.

[0136] The reforming gasoline 26 and the mixed aromatics 37 are processed by the aromatic combined unit 10 (including an aromatic extraction device, a disproportionation-isomerization device and a C8 separation device) to obtain benzene 39, xylene 40, C9+aromatics 41 and the aromatic raffinate 38.

[0137] The hydrogen production raw material 12 (natural gas) is introduced into the hydrogen production unit 11 to obtain hydrogen 13, which provides the required hydrogen for the naphtha hydrogenation unit 4, the diesel hydrocracking unit 6, the wax oil hydrocracking unit 7 and the residual oil hydrocracking unit 8.

[0138] The products obtained in Example 1 and their indexes are listed in Table 1 below.

[0139] Example 2

[0140] The method of Example 1 is followed, except that the processing raw material is a heavy crude oil with an API degree of 27.5 and a sulfur content of 3.1 wt%. The products obtained in Example 2 and their indexes are listed in Table 1 below.

[0141] Comparative Example 1

[0142] Conventional refinery crude oil processing method in the art

[0143] The process shown in FIG. 1 is followed, specifically including the following steps: Figure 2

[0144] (1) The heavy crude oil 42 of Example 2 is introduced into the atmospheric and vacuum distillation device 43 for distillation to obtain liquefied gas 54, naphtha 55, aviation kerosene fraction 56, diesel 57, wax oil 58 and heavy oil 59;

[0145] (2) The liquefied gas 54 and the naphtha 55 are processed by the light hydrocarbon recovery device 44 to obtain light hydrocarbon recovery liquefied gas 60 and light hydrocarbon recovery naphtha 61;

[0146] ​(3) The light hydrocarbon recovery naphtha 61, coking naphtha 80 is hydrogenated by naphtha hydrogenation device 45 to obtain naphtha hydrogenation liquefied gas 62, topping oil 63, hydrogenated heavy naphtha 64; the naphtha hydrogenation treatment conditions include: the reaction temperature is 285℃, the reaction pressure is 2.5MPa, the volume space velocity is 5.5h -1 , the naphtha hydrogenation catalyst is RS-40 catalyst developed by Petroleum Chemical Industry Science Research Institute;

[0147] (4) The aviation coal fraction 56 is hydrogenated by aviation coal hydrogenation device 48 to obtain hydrogenated aviation coal 68; the aviation coal hydrogenation treatment conditions include: the reaction temperature is 250℃, the reaction pressure is 2MPa, the volume space velocity is 4h -1 , the aviation coal hydrogenation catalyst is RSS-2 catalyst developed by Petroleum Chemical Industry Science Research Institute.

[0148] (5) The diesel 57, coking diesel 81 is introduced into diesel hydrogenation cracking device 47 to process to obtain diesel hydrogenation cracking liquefied gas 70, diesel hydrogenation cracking light naphtha 71, diesel hydrogenation cracking heavy naphtha 72 and hydrogenation cracking aviation coal 73; the diesel hydrogenation cracking conditions include: the reaction temperature is 370℃, the reaction pressure is 10MPa, the volume space velocity is 1.2h -1 ; the diesel hydrogenation cracking catalyst is RIC-3 catalyst developed by Petroleum Chemical Industry Science Research Institute.

[0149] (6) The wax oil 58, coking wax oil 82 is introduced into wax oil hydrogenation cracking device 49 to process to obtain wax oil hydrogenation cracking liquefied gas 75, wax oil hydrogenation cracking light naphtha 76, wax oil hydrogenation cracking heavy naphtha 77, wax oil hydrogenation cracking aviation coal 78 and diesel 79; the wax oil hydrogenation cracking conditions include: the reaction temperature is 375℃, the reaction pressure is 16MPa, the volume space velocity is 0.6h -1 ; the wax oil hydrogenation cracking catalyst is RHC-220 catalyst developed by Petroleum Chemical Industry Science Research Institute.

[0150] (7) The heavy oil 59 is introduced into delayed coking device 50 to process to obtain coking naphtha 80, coking diesel 81, coking wax oil 82 and petroleum coke 90.

[0151] (8) The hydrogenated heavy naphtha 64, diesel hydrogenation cracking heavy naphtha 72 and wax oil hydrogenation cracking heavy naphtha 77 are introduced into reforming device 46 to reform to obtain reforming liquefied gas 65, pentane oil 66 and reforming gasoline 67; the reforming conditions include: the reaction temperature is 520℃, the pressure is 0.4MPa, the mass space velocity is 2.5h -1 . The reforming catalyst is PS-VI catalyst developed by Petroleum Chemical Industry Science Research Institute.

[0152] (9) The reforming gasoline 67 is processed by the aromatics combination device 53 to obtain aromatics products and aromatics raffinate 69; the aromatics products include benzene 85, xylene 86 and C9+aromatics 87.

[0153] (10) The top oil 63, the pentane oil 66 and the aromatics raffinate 69 are isomerized by the isomerization device 51 to obtain isomerized gasoline 74; the isomerization conditions include: the reaction temperature is 165℃, the pressure is 2MPa, the mass space velocity is 1h -1 The isomerization catalyst is RISO-B catalyst developed by Petroleum Chemical Industry Research Institute.

[0154] (11) The hydrogenated aviation kerosene 68, the hydrogenated cracking aviation kerosene 73 and the wax oil hydrogenated cracking aviation kerosene 78 are blended to obtain aviation kerosene 88;

[0155] (12) The diesel oil hydrogenated cracking light naphtha 71, the wax oil hydrogenated cracking light naphtha 76 and the isomerized gasoline 74 are blended to obtain gasoline 89 (vehicle gasoline).

[0156] Among them, the hydrogen production raw material (natural gas) 83 is introduced into the hydrogen production device 52 to obtain hydrogen 84, which provides the required hydrogen for the naphtha hydrogenation device 45, the diesel oil hydrogenation cracking device 47 and the wax oil hydrogenation cracking device 49.

[0157] The products and their indexes obtained in the comparative example 1 are listed in the following table 1.

[0158] Table 1

[0159]

[0160]

[0161] It can be seen from the results in table 1 that, compared with the comparative example 1, the aromatics yield is greatly increased by using the system of the present application for processing heavy crude oil, which can be up to 73.56wt%, and no finished oil (gasoline, kerosene and diesel) is produced, which provides a new scheme for "oil conversion" of the refinery.

[0162] The above describes the preferred embodiments of the present application in detail, but the present application is not limited thereto. Within the technical concept of the present application, various simple modifications can be made to the technical scheme of the present application, including the combination of various technical features in any other suitable manner, and these simple modifications and combinations should also be considered as the disclosed content of the present application, and all fall within the protection scope of the present application.

Claims

1. A system for heavy crude oil processing for multi-aromatics production, characterized by, The system comprises a distillation unit (2), a residue hydrocracking unit (8), a diesel hydrocracking unit (6), a reforming unit (5) and a non-hydro-upgrading unit (9); The distillation unit (2) is used for distilling heavy crude oil with an API degree of 20-31 to obtain straight-run liquefied gas, naphtha fraction, first distillate oil, wax oil fraction and residue fraction; The residue hydrocracking unit (8) is used for residue hydrocracking of the residue fraction from the distillation unit (2) to obtain residue hydrocracking liquefied gas, residue hydrocracking naphtha, residue hydrocracking diesel and residue hydrocracking wax oil; The diesel hydrocracking unit (6) is used for diesel hydrocracking of the first distillate oil from the distillation unit (2) and the residue hydrocracking diesel from the residue hydrocracking unit (8) to obtain diesel hydrocracking liquefied gas, diesel hydrocracking light naphtha and diesel hydrocracking heavy naphtha; The reforming unit (5) is used for reforming of the diesel hydrocracking heavy naphtha from the diesel hydrocracking unit (6) to obtain reforming liquefied gas, pentane oil and reforming gasoline; The non-hydro-upgrading unit (9) is used for non-hydro-upgrading of the diesel hydrocracking light naphtha from the diesel hydrocracking unit (6) and the pentane oil from the reforming unit (5) to obtain mixed aromatic hydrocarbon; The system further comprises a wax oil hydrocracking unit (7) which is used for wax oil hydrocracking of the wax oil fraction from the distillation unit (2) and the residue hydrocracking wax oil from the residue hydrocracking unit (8) to obtain wax oil hydrocracking liquefied gas, wax oil hydrocracking light naphtha and wax oil hydrocracking heavy naphtha; The wax oil hydrocracking light naphtha outlet of the wax oil hydrocracking unit (7) is communicated with the inlet of the non-hydro-upgrading unit (9); The wax oil hydrocracking heavy naphtha outlet of the wax oil hydrocracking unit (7) is communicated with the inlet of the reforming unit (5).

2. The system according to claim 1, wherein The system further comprises a light hydrocarbon recovery unit (3) which is used for light hydrocarbon recovery treatment of the straight-run liquefied gas and the naphtha fraction from the distillation unit (2), the residue hydrocracking liquefied gas from the residue hydrocracking unit (8), the diesel hydrocracking liquefied gas from the diesel hydrocracking unit (6) and the reforming liquefied gas from the reforming unit (5) to obtain light hydrocarbon recovery liquefied gas and light hydrocarbon recovery naphtha.

3. The system according to claim 2, wherein The system further comprises a naphtha hydrogenation unit (4) which is used for hydrogenation treatment of the light hydrocarbon recovery naphtha from the light hydrocarbon recovery unit (3) and the residue hydrocracking naphtha from the residue hydrocracking unit (8) to obtain naphtha hydrogenation liquefied gas, topped oil and hydrogenated heavy naphtha; The naphtha hydrogenation liquefied gas outlet of the naphtha hydrogenation unit (4) is communicated with the inlet of the light hydrocarbon recovery unit (3).

4. The system according to claim 3, wherein The topped oil outlet of the naphtha hydrogenation unit (4) is communicated with the inlet of the non-hydro-upgrading unit (9); The hydrogenated heavy naphtha outlet of the naphtha hydrogenation unit (4) is communicated with the inlet of the reforming unit (5).

5. The system of claim 2, wherein, The wax oil hydrocracking liquefied gas outlet of the wax oil hydrocracking unit (7) is communicated with the inlet of the light hydrocarbon recovery unit (3).

6. The system of any one of claims 1-5, wherein, The system further comprises an aromatic hydrocarbon combination unit (10) for processing the reforming gasoline from the reforming unit (5) and the mixed aromatic hydrocarbon from the non-hydro-upgrading unit (9) to obtain an aromatic hydrocarbon product and an aromatic hydrocarbon raffinate oil. The aromatic hydrocarbon product comprises at least one of benzene, toluene and xylene.

7. The system of any one of claims 1-5, wherein, The sulfur content of the heavy crude oil is 0.01-3 wt%.

8. A method for processing heavy crude oil to produce aromatic hydrocarbon, the method comprising the following steps: (1) distilling the heavy crude oil to obtain straight-run liquefied gas, naphtha fraction, first distillate oil, wax oil fraction and residue fraction; (2) performing residue hydrocracking on the residue fraction obtained in step (1) to obtain residue hydrocracking liquefied gas, residue hydrocracking naphtha, residue hydrocracking diesel and residue hydrocracking wax oil; (3) performing diesel hydrocracking on the first distillate oil obtained in step (1) and the residue hydrocracking diesel obtained in step (2) to obtain diesel hydrocracking liquefied gas, diesel hydrocracking light naphtha and diesel hydrocracking heavy naphtha; (4) performing reforming on the diesel hydrocracking heavy naphtha obtained in step (3) to obtain reforming liquefied gas, pentane oil and reforming gasoline; (5) performing non-hydro-upgrading on the pentane oil obtained in step (4) and the diesel hydrocracking light naphtha obtained in step (3) to obtain mixed aromatic hydrocarbon; The API degree of the heavy crude oil is 20-31. The method further comprises: performing wax oil hydrocracking on the wax oil fraction obtained in step (1) and the residue hydrocracking wax oil obtained in step (2) to obtain wax oil hydrocracking liquefied gas, wax oil hydrocracking light naphtha and wax oil hydrocracking heavy naphtha; then performing light hydrocarbon recovery treatment on the wax oil hydrocracking liquefied gas, non-hydro-upgrading on the wax oil hydrocracking light naphtha and reforming on the wax oil hydrocracking heavy naphtha.

9. The method of claim 8, wherein, The conditions of the residue hydrocracking in step (2) include: reaction temperature is 380-470℃, pressure is 10-25MPa, volume space velocity is 0.05-2h -1 .

10. The method of claim 8, wherein, The conditions of the diesel hydrocracking in step (3) include: reaction temperature is 300-420℃, pressure is 4-13 MPa, volume space velocity is 0.2-5h -1 .

11. The method of claim 8, wherein, The conditions for the reforming in step (4) include a reaction temperature of 460-540°C, a pressure of 0.3-2 MPa, a mass space velocity of 0.5-4 h -1 .

12. The method of claim 8, wherein, The conditions of the non-hydrogen modification in step (5) include a reaction temperature of 300-600℃, a pressure of 0.1-1 MPa, a mass space velocity of 0.3-1 h -1 .

13. The method of any one of claims 8-12, wherein, The method further comprises: performing light hydrocarbon recovery treatment on the straight-run liquefied gas and naphtha fraction obtained in step (1), the residue hydrocracking liquefied gas obtained in step (2), the diesel hydrocracking liquefied gas obtained in step (3) and the reforming liquefied gas obtained in step (4) to obtain light hydrocarbon recovery liquefied gas and light hydrocarbon recovery naphtha; then performing non-hydro-upgrading on the light hydrocarbon recovery liquefied gas.

14. The method of claim 13, wherein, The method further comprises: subjecting the light hydrocarbon recovery naphtha and the residual oil hydrocracking naphtha obtained in step (2) to hydrotreatment to obtain naphtha hydroliquefied gas, topped oil, and heavy naphtha; then subjecting the naphtha hydroliquefied gas to light hydrocarbon recovery treatment, subjecting the topped oil to non-hydro modification, and subjecting the heavy naphtha to reforming.

15. The method of claim 14, wherein, The conditions of the hydroprocessing include: reaction temperature is 200-320℃, pressure is 0.5-4MPa, volume space velocity is 1-15h -1 .

16. The method of any of claims 8-12, wherein, The conditions for the wax oil hydrocracking include: reaction temperature is 320-430℃, pressure is 8-18 MPa, volume space velocity is 0.1-3h -1 .

17. The method of any one of claims 8-12, wherein, The method further comprises: processing the reforming gasoline obtained in step (4) and the mixed aromatic hydrocarbon obtained in step (5) to obtain an aromatic hydrocarbon product and an aromatic hydrocarbon raffinate; and then subjecting the aromatic hydrocarbon raffinate to non-hydro modification. The aromatic hydrocarbon product comprises at least one of benzene, toluene, and xylene.

18. The method of any one of claims 8-12, wherein, The heavy crude oil has a sulfur content of 0.01-3 wt%.

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