CN112745950B

CN112745950B - Method and system for hydrotreating deoiled asphalt

Info

Publication number: CN112745950B
Application number: CN201911054142.5A
Authority: CN
Inventors: 孙淑玲; 杨清河; 聂红; 胡大为; 牛传峰; 贾燕子; 戴立顺; 王振; 户安鹏; 任亮
Original assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Current assignee: Sinopec Research Institute of Petroleum Processing; China Petroleum and Chemical Corp
Priority date: 2019-10-31
Filing date: 2019-10-31
Publication date: 2022-06-24
Anticipated expiration: 2039-10-31
Also published as: CN112745950A

Abstract

The invention relates to the field of hydrocarbon oil processing, and discloses a method and a system for hydrotreating deoiled asphalt, which comprise the following steps: (1) introducing the deoiled asphalt and the aromatic hydrocarbon-containing material flow into a first reaction unit for hydrogenation reaction, wherein the first reaction unit contains an ore-rich precursor material and/or a hydrogenation catalyst, and the first reaction unit is a moving bed-fixed bed hydrogenation combined unit or a moving bed hydrogenation unit; (2) fractionating the liquid phase product from the first reaction unit to obtain a light component and a heavy component; (31) introducing the light components into a second reaction unit for reaction to obtain gasoline components, diesel components and/or BTX raw material components; and (32) introducing the heavies to a delayed coking unit for reaction; or as a low sulfur marine fuel oil component. The treatment process provided by the invention can realize high-value DOA utilization.

Description

Method and system for hydrotreating deoiled asphalt

Technical Field

The invention relates to the field of hydrocarbon oil processing, in particular to a method for hydrotreating de-oiled asphalt and a system for hydrotreating de-oiled asphalt.

Background

The high-efficiency conversion of residual oil is the core of oil refining enterprises. The fixed bed residual oil hydrogenation is a key technology for efficiently converting residual oil, and has the characteristics of good product quality, mature process and the like.

However, the high content of asphaltene and metals in the residual oil is a limiting factor of the operation period of the fixed bed residual oil hydrogenation unit.

In order to solve the problem, a residual oil solvent deasphalting (demetalization) -hydrotreating-catalytic cracking combined process technology (SHF) developed by the research institute of petrochemical and chemical engineering science is an innovative technology for producing clean fuel for vehicles from low-value vacuum residual oil to the maximum extent and prolonging the operation period, but due to the high softening point of deoiled asphaltene (DOA), the transportation and the utilization are difficult, and the popularization of the SHF technology is limited.

The new combined process for producing more propylene by hydrogenating and catalytic cracking (DCC) chemical transformed residual oil is also limited by the influence of asphaltene and metal in the residual oil, the hydrogenated residual oil has low hydrogen content, the residual oil hydrogenation has short running period and low DCC propylene yield, and the economic benefit of the combined technology is influenced.

In addition, in 2020, a new low-sulfur ship fuel standard with a sulfur mass fraction not more than 0.5% and a low-sulfur petroleum coke standard with a sulfur mass fraction not more than 3.0% are implemented, and a technology for producing the low-sulfur ship fuel (low-sulfur petroleum coke) at low cost is also a problem which needs to be solved urgently at present.

Therefore, the conversion of DOA to low sulfur ship fuel or feedstock for low sulfur petroleum coke production is a technical challenge that needs to be addressed.

Disclosure of Invention

The invention aims to overcome the defects of the prior art and provide a method and a system for hydrotreating deoiled asphalt, which can realize high-value utilization of DOA.

In order to achieve the above object, a first aspect of the present invention provides a method for hydrotreating deoiled asphalt, comprising:

(1) introducing deoiled asphalt and an aromatic hydrocarbon-containing material flow into a first reaction unit to carry out hydrogenation reaction, wherein the first reaction unit contains an ore-rich precursor material and/or a hydrogenation catalyst, the hydrogenation catalyst can catalyze at least one reaction selected from hydrodemetallization reaction, hydrodesulfurization reaction, hydrodeasphaltization reaction and hydrodecarbonization reaction, the first reaction unit is a moving bed-fixed bed hydrogenation combination unit or a moving bed hydrogenation unit, the dosage ratio of the deoiled asphalt and the aromatic hydrocarbon-containing material flow is that a mixed raw material formed by the deoiled asphalt and the aromatic hydrocarbon-containing material flow is in a liquid state at the temperature of not higher than 400 ℃, and the ore-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca and Mg;

(2) fractionating a liquid-phase product from the first reaction unit to obtain a light component and a heavy component, wherein the cutting points of the light component and the heavy component are 240-450 ℃;

(31) introducing the light components into a second reaction unit for reaction to obtain at least one product selected from a gasoline component, a diesel component and a BTX raw material component, wherein the second reaction unit is selected from at least one of a hydrocracking unit, a catalytic cracking unit and a diesel hydro-upgrading unit; and

(32) introducing the heavy components into a delayed coking unit for reaction to obtain at least one product selected from the group consisting of coker gasoline, coker diesel, coker gas oil, and low sulfur petroleum coke; or as a low sulfur marine fuel oil component.

A second aspect of the present invention provides a system for hydroprocessing deoiled asphalt, comprising:

the first reaction unit is a moving bed-fixed bed hydrogenation combined unit or a moving bed hydrogenation unit and is used for carrying out hydrogenation reaction on the deoiled asphalt and the aromatic hydrocarbon-containing material flow;

a separation unit in fluid communication with the first reaction unit for fractionating therein a liquid phase product from the first reaction unit;

a second reaction unit in fluid communication with the separation unit for reacting therein the light components obtained from the separation unit, the second reaction unit being selected from at least one of a hydrocracking unit, a catalytic cracking unit, and a diesel hydro-upgrading unit;

a delayed coking unit in fluid communication with the separation unit for reacting heavy components obtained from the separation unit therein to yield at least one product selected from the group consisting of coker gasoline, coker diesel, coker gas oil, and low sulfur petroleum coke;

an outlet in fluid communication with the separation unit for withdrawing heavy components obtained from the separation unit out of the system as a low sulfur bunker fuel oil component.

The DOA is subjected to hydrotreating (e.g., hydrodesulfurization) together with an aromatic-containing stream by a moving bed-fixed bed hydrogenation combination unit or by a moving bed hydrogenation unit, and the hydrogenated light components are subjected to hydrocracking (RLG or RLA) to produce BTX, gasoline fractions and diesel fractions, or catalytic cracking (LTAG) to produce gasoline fractions (and liquefied gas); and (3) producing heavy low-sulfur ship fuel or low-sulfur petroleum coke from the hydrogenated heavy components.

The treatment process provided by the invention can realize high-value DOA utilization.

In addition, the vanadium-rich material obtained in the method of the invention can be used for refining high-value V₂O₅。

Drawings

FIG. 1 is a process flow diagram of a hydroprocessing deoiled asphalt according to a preferred embodiment of the present invention.

Description of the reference numerals

1 heavy oil raw material 2 solvent deasphalting unit

3 deasphalted oil 4 deoiled asphalt

5 aromatic hydrocarbon-containing material flow 6 mixed raw material

7 first reaction unit 8 light component

9 heavy component 10 second reaction unit

11 delayed coking unit 12 BTX feedstock composition

13 gasoline component 14 Diesel component

15 coking gasoline and 16 coking diesel oil

17 coking wax oil 18 low sulfur petroleum coke

19 separation unit

Detailed Description

The endpoints of the ranges and any values disclosed herein are not limited to the precise range or value, and such ranges or values should be understood to encompass values close to those ranges or values. For ranges of values, between the endpoints of each of the ranges and the individual points, and between the individual points may be combined with each other to give one or more new ranges of values, and these ranges of values should be considered as specifically disclosed herein.

As previously mentioned, a first aspect of the present invention provides a process for hydroprocessing deoiled asphalt, comprising:

Preferably, the deoiled asphalt and the aromatic hydrocarbon-containing stream are used in a ratio such that a mixed feedstock formed from the deoiled asphalt and the aromatic hydrocarbon-containing stream is in a liquid state at a temperature of not higher than 280 ℃; it is further preferred that the deoiled bitumen and the aromatic hydrocarbon-containing stream are used in such a ratio that the mixed feedstock formed from the deoiled bitumen and the aromatic hydrocarbon-containing stream is in a liquid state at a temperature of not higher than 100 ℃.

Particularly preferably, the cut point of the light fraction and the heavy fraction is 350 ℃.

Preferably, in step (1), the deoiled asphalt and the aromatic hydrocarbon-containing stream are used in such a ratio that the viscosity at 100 ℃ of the mixed feedstock formed by the deoiled asphalt and the aromatic hydrocarbon-containing stream is not more than 400mm²S, more preferably not more than 200mm²S, further preferably not more than 100mm²/s。

Preferably, in step (1), the aromatic hydrocarbon-containing stream is a distillate oil rich in aromatic hydrocarbons and/or aromatic hydrocarbon compounds.

Preferably, the end point of the aromatics-rich distillate is at 200-540 ℃ and the aromatics content is equal to or greater than 20 wt.%, preferably equal to or greater than 40 wt.%, more preferably equal to or greater than 50 wt.%.

Preferably, the distillate oil rich in aromatic hydrocarbon is at least one selected from LCO, HCO, ethylene tar, coal tar, coker diesel oil and coker gas oil. The distillate rich in aromatic hydrocarbons according to the present invention may be obtained from a process other than the process according to the present invention, or may be obtained from the process according to the present invention.

Preferably, the aromatic hydrocarbon compound is selected from one or more of benzene, toluene, xylene, naphthalene, methylnaphthalene, multi-branched naphthalene and aromatic hydrocarbon with more than two rings, and polycyclic aromatic hydrocarbon with no more than three rings or a mixture thereof is preferred. Particularly preferably, the aromatic hydrocarbon compound is selected from benzene, toluene, xylene, naphthalene, a mixture of at least one C_1-6At least one of alkyl substituted naphthalene and aromatic hydrocarbon with more than three rings.

According to a preferred embodiment, in step (1), the aromatic-containing stream is an aromatic-rich distillate, and the mass ratio of the amount of the deoiled asphalt to the amount of the aromatic-containing stream is from 1:10 to 50:10, more preferably from 3:10 to 30: 10.

According to another preferred embodiment, in the step (1), the aromatic hydrocarbon-containing material flow is aromatic hydrocarbon compounds, and the mass ratio of the deoiled asphalt to the aromatic hydrocarbon compounds is 1: 10-50: 10; more preferably from 3:10 to 20: 10.

Preferably, in the step (1), the deoiled asphalt is obtained by subjecting a heavy oil raw material to a solvent deasphalting treatment in a solvent deasphalting unit.

Preferably, in the solvent deasphalting unit, the mass fraction of the yield of the deoiled asphalt is not more than 50%, more preferably not more than 40%, and still more preferably not more than 30%.

Preferably, the method of the present invention further comprises: recycling the coker diesel and/or coker wax obtained in step (32) back to step (1) as at least part of the aromatic-containing stream.

The first reaction unit is a moving bed-fixed bed hydrogenation combined unit or a moving bed hydrogenation unit. In a first preferred case, the first reaction unit is a moving bed-fixed bed hydrogenation combination unit; in a second preferred aspect, the first reaction unit is a moving bed hydrogenation unit.

According to the invention, the first reaction unit is particularly preferably a moving bed-fixed bed hydrogenation combined unit.

Preferably, in step (1), the operating conditions in the first reaction unit include: the reaction temperature is 280-450 ℃, the reaction pressure is 8.0-20.0 MPa, the volume ratio of hydrogen to oil is 400-2000, and the liquid hourly space velocity is 0.05-1.2 h^-1(ii) a More preferably, the operating conditions in the first reaction unit include: the reaction temperature is 330-420 ℃, the reaction pressure is 10.0-18.0 MPa, the volume ratio of hydrogen to oil is 600-1200, and the liquid hourly space velocity is 0.10-0.8 h^-1. The liquid hourly space velocity and reaction pressure are selected according to the characteristics of the material to be treated and the desired conversion and refining depth.

Unless otherwise specified, all pressures described herein are expressed as gauge pressure.

According to a preferred embodiment, in step (1), the first reaction unit is a moving bed-fixed bed hydrogenation combination unit, and the moving bed is filled with the ore-rich precursor material, and the fixed bed is sequentially filled with the ore-rich precursor material and the hydrogenation catalyst or the fixed bed is filled with the hydrogenation catalyst.

Preferably, in step (1), the first reaction unit is a moving bed-fixed bed hydrogenation combination unit, and the moving bed is filled with the ore-rich precursor material and the hydrogenation catalyst in sequence, and the fixed bed is filled with the ore-rich precursor material and the hydrogenation catalyst in sequence or the fixed bed is filled with the hydrogenation catalyst.

In the aforementioned preferred embodiment, more preferably, the ratio of the volume of the mineral-rich precursor material charged in the moving bed to the sum of the volumes of the mineral-rich precursor material and the hydrogenation catalyst charged in the fixed bed is 10:90 to 60:40, preferably 20:80 to 40: 60. It should be explained that, when the fixed bed is packed with only the hydrogenation catalyst, the above packed volume ratio represents: the ratio of the volume of the ore-rich precursor material loaded in the moving bed to the volume of the hydrogenation catalyst loaded in the fixed bed.

Preferably, the method of the present invention further comprises: and replacing the ore-rich precursor material filled in the moving bed with a fresh ore-rich precursor material in each period, wherein the replacement proportion accounts for 5-20 mass percent of the total amount of the ore-rich precursor material filled in the moving bed, and is more preferably 10-15 mass percent.

Preferably, the period is 5-20 days, preferably 10-15 days.

Preferably, in step (1), the ore-rich precursor material contains a carrier and an active component element loaded on the carrier, the carrier is selected from at least one of aluminum hydroxide, aluminum oxide and silicon oxide, and the active component element is selected from at least one of metal elements in groups VIB and VIII. More preferably, the active component in the mineral-rich precursor material is an oxide and/or sulfide of a metal element selected from groups VIB and VIII.

The shape of the mineral-rich precursor material of the present invention may be cylindrical and/or spherical, preferably spherical.

Preferably, the average particle size of the mineral-rich precursor material is 0.1 to 6mm, more preferably 0.3 to 4mm, and still more preferably 0.5 to 1.5 mm.

The fresh rich mineral precursor material used for replacing the rich mineral precursor material filled in the moving bed is in an oxidized state or a vulcanized state, preferably a vulcanized state.

More preferably, in the step (1), the rich-ore precursor material has a scorch reduction of not less than 3% by mass and a specific surface area of not less than 80m²(ii) water absorption of not less than 0.9 g/g. The ignition reduction refers to the mass percentage of the reduced mass of the ore-rich precursor material after 600 ℃/2h roasting treatment to the mass before roasting; the water absorption rate refers to the percentage of the mass of the ore-rich precursor material which is increased in the soaking water for half an hour at room temperature (for example, 25 ℃) to the mass before soaking.

According to a preferred embodiment, in step (1), the first reaction unit is sequentially charged with a first ore-rich precursor material and a second ore-rich precursor material in terms of the reactant flow direction, and the ignition loss of the second ore-rich precursor material is equal to or greater than that of the first ore-rich precursor material. The present invention is not particularly limited to the specific filling positions of the first and second rich precursor materials, as long as: and (3) relative to a second ore-rich precursor material, the reaction material is firstly contacted with the first ore-rich precursor material and then contacted with the second ore-rich precursor material.

According to the foregoing preferred embodiment, it is further preferred that the first mineral-rich precursor material has a burn reduction of 3 to 15 mass%, and the second mineral-rich precursor material has a burn reduction of not less than 15 mass%.

According to the foregoing preferred embodiment, it is further preferred that the packing volume ratio of the first and second rich precursor materials is from 5:95 to 95: 5.

The hydrogenation catalyst of the present invention may be a graded combination of different catalysts, preferably the hydrogenation catalyst is at least capable of catalyzing hydrodemetallization and hydrodesulfurization reactions.

The present invention is not particularly limited with respect to the specific type of catalyst capable of catalyzing the hydrodemetallization reaction, hydrodesulfurization reaction, hydrodeasphaltization reaction, and hydrodecarbonization reaction, and a catalyst capable of catalyzing the above reaction, which is conventionally used in the art, may be used.

The hydrogenation catalyst of the present invention may be, for example, a catalyst in which a porous refractory inorganic oxide is used as a carrier, and an oxide or sulfide of a group VIB and/or group VIII metal is used as an active component, and an auxiliary is selectively added.

Preferably, after the first reaction unit of the invention is operated for a long period, the ore-rich precursor material is converted into a vanadium-rich material, and the content of vanadium in the vanadium-rich material is not less than 10 wt%.

Preferred embodiments in the first reaction unit of the present invention are provided below:

the raw material hydrotreating technology involved in the first reaction unit of the present invention is a moving bed-fixed bed hydrotreating technology or a moving bed hydrotreating technology. Wherein, the moving bed reactor is filled with spherical ore-rich precursor materials, and the average grain diameter of the spherical catalyst is 0.1-6 mm. The fixed bed reaction bed layer at least comprises an ore-rich precursor material and/or a hydrogenation catalyst, and the ore-rich precursor material mainly comprises two parts: the carrier has strong capability of adsorbing vanadium-containing organic compounds in oil, and the active component has a hydrogenation activity function. The reactor or the reaction bed layer at least comprises an ore-rich precursor material and a hydrogenation catalyst, wherein the ore-rich precursor material mainly comprises two parts: the carrier has strong capability of adsorbing vanadium-containing organic compounds in oil, and the active component has a hydrogenation activity function. The carrier is mainly obtained by extruding, molding and drying silicon oxide, aluminum hydroxide or aluminum hydroxide/aluminum oxide mixture, the surface of the carrier is rich in-OH, the carrier has strong adsorption capacity on vanadium-containing organic compounds in oil, and the ignition loss of the carrier is not less than 5 mass percent after roasting for 2 hours at 600 ℃. The active component mainly adopts oxides or sulfides of metals of VIB group and/or VIII group such as W, Mo, Co, Ni and the like.

The hydrogenation catalyst referred to in the foregoing preferred embodiment is generally a heavy residue hydrogenation catalyst, and the heavy residue hydrogenation catalyst used refers to a combined catalyst having functions of heavy residue and residue hydrodemetallization, hydrodesulfurization, hydrodecarbonization and the like. These catalysts are generally catalysts in which a porous refractory inorganic oxide such as alumina is used as a carrier, oxides or sulfides of metals of group VIB and/or group VIII such as W, Mo, Co, Ni and the like are used as active components, and other various assistants such as elements P, Si, F, B and the like are selectively added, such as RDM, RCS series heavy metals, residual oil hydrodemetallization catalysts and desulfurization catalysts developed by petrochemical engineering research institute. At present, in the fixed bed and/or moving bed residual oil hydrogenation technology, a plurality of catalysts are often used together. In the present invention, a rich mineral precursor material, a hydrodemetallation desulfurization catalyst and a hydrodesulfurization catalyst are preferably used, and the loading order is generally that the raw material is sequentially contacted with the rich mineral precursor material, the hydrodemetallation desulfurization and the hydrodesulfurization catalyst, and one or two catalysts may be less loaded according to circumstances, for example, only the rich mineral precursor material and the hydrodesulfurization catalyst are loaded, but the hydrodemetallation desulfurization catalyst is not loaded. Of course, there is a technique of mixing and packing these catalysts.

Preferably, in step (31), the second reaction unit is a hydrocracking unit, and theThe operating conditions in the hydrocracking unit include: the reaction temperature is 330-420 ℃, the reaction pressure is 5.0-18.0 MPa, the volume ratio of hydrogen to oil is 500-2000, and the liquid hourly space velocity is 0.3-3.0 h^-1。

Preferably, the hydrocracking unit is packed with at least one hydrotreating catalyst and at least one hydrocracking catalyst.

Preferably, the hydrocracking unit is a fixed bed hydrocracking unit.

Preferred embodiments in the second reaction unit of the present invention are provided below:

in the step (31), the light components are introduced into a second reaction unit for reaction, and the adopted hydrocracking technology is fixed bed hydrocracking technology. Taking the industrial mature fixed bed wax oil hydrocracking technology as an example, the reactor or the reaction bed layer at least comprises two hydrocracking catalysts, one is a pretreatment catalyst and the other is a hydrocracking catalyst. Because the metal content, the sulfur content, the nitrogen content and the carbon residue value of the material obtained by fractionation after the fixed bed hydrogenation treatment are all higher, the pretreatment catalyst preferably has strong demetallization activity and good desulfurization and denitrification activity so as to ensure the activity of the subsequent hydrocracking catalyst. The hydrocracking catalyst preferably has good hydrocracking activity. These catalysts are generally catalysts in which a porous refractory inorganic oxide such as alumina or molecular sieve is used as a carrier, oxides of metals of the VIB group and/or VIII group such as W, Mo, Co, Ni and the like are used as active components, and other various additives such as P, Si, F, B and the like are selectively added, for example, RS series pretreatment catalysts and RHC series hydrocracking catalysts developed by the institute of petrochemical engineering science and technology belong to the catalysts. The RS series catalyst is a NiW catalyst, and the RHC series catalyst is a NiMo molecular sieve catalyst.

Preferably, in step (31), the second reaction unit is a catalytic cracking unit, and the catalytic cracking unit is a Fluid Catalytic Cracking (FCC) unit.

Preferably, the light component catalytic cracking technology used in the light component catalytic cracking is FCC technology, preferably LTAG technology developed by the institute of petrochemical science and technology, and mainly produces gasoline fractions and liquefied gas.

Preferably, the operating conditions in the fluid catalytic cracking unit include: the reaction temperature is 500-600 ℃, the agent-oil ratio is 3-12, and the retention time is 1-10 s; more preferably, the operating conditions of the fluid catalytic cracking unit include: the reaction temperature is 520-580 ℃, the agent-oil ratio is 4-10, and the retention time is 2-5 s.

The agent-oil ratio of the invention is expressed by the mass ratio of the agent-oil.

Preferably, in step (31), the second reaction unit is a diesel hydrogenation upgrading unit, and the operating conditions in the diesel hydrogenation upgrading unit include: the reaction temperature is 330-420 ℃, the reaction pressure is 5.0-18.0 MPa, the volume ratio of hydrogen to oil is 500-2000, and the liquid hourly space velocity is 0.3-3.0 h^-1。

Preferably, the diesel hydro-upgrading unit is loaded with at least one diesel hydro-upgrading catalyst.

The diesel hydrogenation upgrading catalyst can be a combined catalyst with functions of diesel hydrodesulfurization, hydrodenitrogenation and the like, for example. These catalysts are generally catalysts in which a porous refractory inorganic oxide such as alumina is used as a carrier, oxides or sulfides of metals of group VIB and/or group VIII such as W, Mo, Co, Ni and the like are used as active components, and other various additives such as P, Si, F, B and the like are selectively added, such as RS series diesel hydrodesulfurization catalysts and denitrification catalysts developed by petrochemical engineering science research institutes.

Preferably, in step (32), the heavy components are introduced into a delayed coking unit for reaction to obtain at least one product selected from the group consisting of coker gasoline, coker diesel, coker gas oil and low sulfur petroleum coke, and the operating conditions to the delayed coking unit include: the reaction temperature is 440-520 ℃, and the retention time is 0.1-4 h.

Preferably, in step (32), the heavies are introduced to a delayed coking unit for reaction to produce low sulfur petroleum coke, and conditions are controlled such that the sulfur content of the heavies is no greater than 1.8 wt.%, more preferably the sulfur content of the low sulfur petroleum coke is no greater than 3 wt.%.

Preferably, in step (32), the heavy fraction is used as a low sulfur bunker fuel oil fraction and the conditions are controlled such that the sulfur content of the low sulfur bunker fuel oil fraction is no greater than 0.5 wt.%.

The present invention is not particularly limited with respect to the specific operation of the solvent deasphalting treatment, and may be carried out by a solvent deasphalting process which is conventional in the art. The operating parameters of the solvent deasphalting process are exemplified in the examples of the present invention and those skilled in the art should not be construed as limiting the invention.

The invention is suitable for the hydroconversion of normal slag and slag reduction, and is particularly suitable for the hydroconversion of poor residual oil of high metal (Ni + V >150 mug/g, particularly Ni + V >200 mug/g), high carbon residue (the mass fraction of the carbon residue is >17 percent, particularly the mass fraction of the carbon residue is >20 percent) and high condensed ring substances.

As previously mentioned, a second aspect of the present invention provides a system for hydroprocessing deoiled asphalt, comprising:

a separation unit in fluid communication with the first reaction unit for fractionating a liquid phase product from the first reaction unit therein;

Preferably, said delayed coking unit is in fluid communication with said first reaction unit for recycling said coker gas oil and/or said coker gas oil obtained in said delayed coking unit back to said first reaction unit.

Preferably, the system further comprises a solvent deasphalting unit, which is in fluid communication with the first reaction unit and is used for introducing the deoiled asphalt obtained after the solvent deasphalting treatment of the heavy oil raw material in the solvent deasphalting unit into the first reaction unit.

According to a preferred embodiment, in the system of the invention, the second reaction unit is a hydrocracking unit.

According to another preferred embodiment, in the system of the present invention, the second reaction unit is a catalytic cracking unit and the catalytic cracking unit is a fluid catalytic cracking unit.

According to another preferred embodiment, in the system of the present invention, the second reaction unit is a diesel hydro-upgrading unit.

The process for hydrotreating deoiled asphalt of the present invention is further described in detail below with reference to fig. 1.

As shown in fig. 1, heavy oil raw material 1 enters solvent deasphalting unit 2 to obtain deasphalted asphalt 4 and deasphalted oil 3 after solvent deasphalting treatment; the deoiled asphalt 4 and the aromatic hydrocarbon-containing material flow 5 form a mixed raw material 6 and enter a first reaction unit 7 for hydrogenation reaction, wherein the first reaction unit contains an ore-rich precursor material and/or a hydrogenation catalyst, and the first reaction unit is a moving bed-fixed bed hydrogenation combined unit or a moving bed hydrogenation unit; fractionating a liquid-phase product from the first reaction unit to obtain a light component 8 and a heavy component 9, wherein the cutting point of the light component and the heavy component is 330-380 ℃; introducing the light component 8 into a second reaction unit 10 for reaction to obtain at least one product selected from a gasoline component 13, a BTX raw material component 12 and a diesel oil component 14, wherein the second reaction unit is selected from at least one of a hydrocracking unit, a catalytic cracking unit and a diesel oil hydrogenation upgrading unit; and introducing the heavy fraction 9 into a delayed coking unit 11 for reaction to obtain at least one product selected from the group consisting of coker gasoline 15, coker diesel 16, coker gas oil 17, and low sulfur petroleum coke 18; or the heavies 9 as a low sulfur marine fuel oil component.

The present invention relates to a refining and conversion process of heavy hydrocarbon with high asphaltene, colloid, sulfur and metal content, including heavy oil and residual oil hydrogenation process, hydrocracking process or catalytic cracking process and coking process, and is characterized by that said combined process not only can be adapted to the heavy conversion and degradation of raw oil, and can increase the treatment capacity of heavy oil and residual oil, but also can raise the yield of gasoline and chemical material, and can produce high-quality low-sulfur ship fuel component and low-sulfur petroleum coke raw material or low-sulfur petroleum coke.

Compared with the prior art, the invention preferably adopts the organic combination of the processes of solvent deasphalting, heavy oil hydrogenation, hydrocracking, catalytic cracking or coking and the like, so that not only the light petroleum fraction is utilized with high value, but also the DOA with low value is converted into the low-sulfur ship fuel component and the low-sulfur petroleum coke raw material which meet the environmental protection requirement, thereby realizing the high-efficiency, environmental protection and comprehensive utilization of the heavy petroleum resource.

The present invention will be described in detail below by way of examples. The following examples were carried out using the process flow shown in FIG. 1, unless otherwise specified.

The results of table 2 in the following examples are, without specific mention, the average of the results obtained in the sampling test every 25h in the continuous operation of the apparatus for 100 h.

The catalytic cracking catalysts MLC-500, RS-2100 hydrofining catalyst, RHC-131 hydrocracking catalyst, RG-30B, RDM-33B and RCS-31 are all produced by Changjingtong division of China petrochemical catalyst Limited.

The properties of the aromatics-rich distillate used in each example are shown in Table 6.

The normal temperature referred to below means 25. + -. 3 ℃.

Example A

Preparation of the ore-rich precursor material 1: selecting 2000g of RPB110 pseudo-boehmite produced by Changjingtian division of China petrochemical catalyst Limited, treating 1000g of the RPB110 pseudo-boehmite at 550 ℃ for 2h to obtain about 700g of alumina, fully mixing about 700g of alumina and 1000g of pseudo-boehmite, adding 40g of sesbania powder and 20g of citric acid, adding 2200g of deionized water, kneading, extruding into strips, drying at 300 ℃ for 3h to obtain about 1730g of carrier, adding 2100mL of solution containing Mo and Ni for saturated impregnation, wherein the Mo content in the solution is MoO₃5.5% by weight and 1.5% by weight of Ni, based on the weight of NiO, were impregnated for half an hour, followed by treatment at 180 ℃ for 4h to give a mineral-rich precursor material 1, the properties of which are shown in table 5.

Preparation of the ore-rich precursor material 2: selecting 2000g of RPB110 pseudo-boehmite produced by Changling division of China petrochemical catalyst Limited company, adding 30g of sesbania powder and 30g of citric acid, adding 2400g of deionized water, kneading, extruding into strips, drying at 120 ℃ for 5 hours to obtain about 2040g of carrier, adding 2200mL of solution containing Mo and Ni for saturated dipping, wherein the content of Mo in the solution is MoO₃7.5% by weight and a Ni content of 1.7% by weight of NiO, were impregnated for half an hour and then treated at 200 ℃ for 3 hours to obtain a mineral-rich precursor material 2, properties of which are shown in table 5.

Preparation of the ore-rich precursor material 3: selecting 2000g of commercially available silicon oxide, adding 30g of sesbania powder and 30g of sodium hydroxide, adding 2400g of deionized water, kneading, extruding into strips, forming, drying at 120 ℃ for 5 hours to obtain about 2000g of carrier, adding 2200mL of solution containing Mo and Ni for saturated impregnation, wherein the content of Mo in the solution is MoO₃4.5% by weight and a Ni content of 1.0% by weight of NiO, were impregnated for half an hour and then treated at 200 ℃ for 3 hours to obtain a mineral-rich precursor material 3, properties of which are shown in table 5.

Example B

Solvent deasphalting is carried out by taking middle east vacuum residuum as raw material, using a hydrocarbon mixture mainly containing butane (butane content is 75 wt%) and containing a small amount of propane and pentane, and reacting at 120 ℃ in the presence of a solvent: vacuum residue 1.5: 1 (mass ratio), the mass yield of deasphalted oil (DAO) is 68.1%, and the mass yield of deoiled asphalt (DOA) is 31.9%.

Example 1

Raw materials:the DOA and the LCO in the embodiment B are mixed according to the mass ratio of 1:10, the mixed raw materials are liquid at normal temperature, and the properties of the mixed raw materials are shown in Table 1.

A first reaction unit:the mixed raw materials were tested on a medium-sized moving bed-fixed bed heavy oil hydrotreater. Filling an ore-rich precursor material 1 in a moving bed reactor, filling an ore-rich precursor material 2, an RDM-33B residual oil demetalization desulfurization transition catalyst and an RCS-31 desulfurization catalyst in a fixed bed reactor according to the flow direction of reactants, wherein the filling volume ratio is as follows: rich-ore precursor material 1: ore-rich precursor material 2: RDM-33B: RCS-31 ═ 30: 36: 14: 20. the operating conditions of the hydrotreatment are as follows: pressure of 16MPa and space velocity of 0.18h^-1Hydrogen/oil ratio (volume): 1000: 1, wherein the hydrogenation reaction temperature of the moving bed reactor is 385 ℃, and the hydrogenation reaction temperature of the fixed bed reactor is 370 ℃. The product properties after hydrotreating of the mixed feed are shown in table 2.

Separation:the properties of the heavy components at 335 ℃ or higher in the liquid phase product obtained by fractionation and hydrotreatment are shown in Table 3.

A second reaction unit:carrying out a hydrocracking test on the light components with the temperature of less than 335 ℃ on a fixed bed hydrocracking device, wherein the filling ratio of the catalyst is as follows: RS-2100, RHC-131 ═ 40:60 (V/V), and the hydrocracking process conditions are as follows: the temperature of the refining section is 370 ℃, the temperature of the cracking section is 385 ℃, the pressure is 7MPa, and the space velocity is 2.0h^-1Hydrogen/oil (volume): 1200: 1, the properties of the obtained hydrocracked gasoline product are shown in table 4.

Example 2

Raw materials:DOA and HCO in the embodiment B are mixed according to the mass ratio of 5:10, the mixed raw material is liquid at normal temperature, and the properties of the mixed raw material are shown in Table 1.

A first reaction unit:medium-sized moving bed-fixed bed for mixed raw materialsThe tests were carried out on a heavy oil hydrotreater under the same catalyst loading and process conditions as in example 1, and the product properties after hydrotreatment are shown in Table 2.

Separation:the properties of the heavy components at 378 ℃ or higher of the liquid phase product obtained by the fractional distillation and the hydrotreatment are shown in Table 3.

A second reaction unit:the light component below 378 ℃ was tested in a fixed bed hydrocracking unit under the same catalyst and test conditions as in the light component hydrocracking test of example 1 to obtain a hydrocracked product, the properties of which are shown in table 4.

Example 3

Raw materials:the DOA and the LCO in the embodiment B are mixed according to the mass ratio of 10:10, the mixed raw materials are liquid at normal temperature, and the properties of the mixed raw materials are shown in Table 1.

A first reaction unit:the mixed raw materials were tested on a medium-sized moving bed-fixed bed heavy oil hydrotreater under the same catalyst loading and process conditions as in example 1, and the product properties after hydrotreatment are shown in table 2.

Separation:the properties of the heavy components at 350 ℃ or higher in the liquid phase product obtained by fractionation and hydrotreatment are shown in Table 3.

A second reaction unit:the light component at a temperature of less than 350 ℃ was tested on a fixed bed hydrocracking unit under the same catalyst and test conditions as in the light component hydrocracking test of example 1 to obtain a hydrocracked product, the properties of which are shown in table 4.

Example 4

Raw materials:the DOA and the coal tar I in the embodiment B are mixed according to the mass ratio of 15:10, the mixed raw material is in a liquid state at normal temperature, and the properties of the mixed raw material are shown in Table 1.

Separation:the properties of the heavy components at 355 ℃ or higher in the liquid phase product obtained by the fractionation and the hydrotreatment are shown in Table 3.

A second reaction unit:the light component below 355 ℃ was tested in a fixed bed hydrocracking unit under the same catalyst and test conditions as in the light component hydrocracking test of example 1 to obtain a hydrocracked product, the properties of which are shown in table 4.

Example 5

A similar procedure was followed as in example 3, except that:

a first reaction unit:in this example, the moving bed hydrogenation reaction temperature was 395 ℃ and the fixed bed hydrogenation reaction temperature was 385 ℃.

The remaining conditions were the same as in example 3.

The properties of the resulting heavy components at temperatures of 350 ℃ and above are shown in Table 3.

Example 6

Raw materials:as in example 3.

A first reaction unit:the catalyst loading and hydrotreating operating conditions were the same as in example 5.

And replacing the ore-rich precursor material 1 in the moving bed reactor once by using the vulcanized ore-rich precursor material 1 every 14 days, wherein the volume of each replacement is 5%, the fixed bed hydrogenation reaction temperature is increased by 0.5 ℃ every 30 days, the operation is stopped after the hydrogenation test is operated for 500 days in total, and the mass fraction of the oil sulfur generated by hydrogenation is 0.40-0.50%.

The vanadium-rich material 1 and the vanadium-rich material 2 are obtained by initially loading the vanadium-rich precursor material 1 and the vanadium-rich precursor material 2 into a reactor, reacting the materials to obtain the vanadium-rich material 1 and the vanadium-rich material 2, and analyzing the vanadium-rich material 1 after roasting, wherein the average vanadium content of the vanadium-rich material 1 is 69 mass percent, the vanadium content of the vanadium-rich material 2 is 75 mass percent, and the vanadium-rich material is a high-value V extraction₂O₅High quality material of (2).

Example 7

Heavy components of 350 ℃ or higher in example 3 are introduced into a delayed coking unit for coking treatment, and the conditions in the delayed coking unit comprise: the reaction temperature was 490 ℃ and the residence time 1.5 h.

The mass yield of the low-sulfur petroleum coke is 26.3%, and the mass fraction of sulfur in the petroleum coke is 2.6%.

Example 8

The light fraction below 350 ℃ of example 3 was subjected to a catalytic cracking test in a small catalytic cracking fixed fluid bed test unit using a catalytic cracking catalyst MLC-500, the conditions of the fluid catalytic unit comprising: the reaction temperature was 540 ℃, the agent-to-oil ratio was 6, and the average residence time was 3 s.

As a result, the product gasoline mass yield is 57.3%, and the RON octane number of the gasoline is 95.3.

Example 9

Raw materials:the mixed raw materials were the same as in example 3.

A first reaction unit:similar to example 3, except that the catalyst was loaded, in this example, the moving bed reactor of the first reaction unit was loaded with the ore-rich precursor material 1: mineral-rich precursor material 2 ═ 35:65 (V/V); the RDM-33B residual oil demetalization desulfurization transition catalyst and the RCS-31 desulfurization catalyst are filled in the fixed bed reactor of the first reaction unit, and the filling volume ratio is as follows: RDM-33B: RCS-31 ═ 45: 55. the conditions and process of hydrotreating the mixed feed were the same as in example 1. After hydrotreatment, the product properties are shown in Table 2.

Replacing the rich ore precursor material in the moving bed reactor once by using a sulfurized rich ore precursor material 1 and a sulfurized rich ore precursor material 2 every 14 days, wherein the volume of each replacement is 5%, wherein the sulfurized rich ore precursor material 1: the sulfidic rich precursor material 2 is 35: 65.

And every 30 days, the reaction temperature of the fixed bed reactor is increased by 3 ℃, the operation is stopped after the hydrogenation test is carried out for 330 days in total, the mass fraction of sulfur in the oil generated by hydrogenation is 0.55-0.65%, and the content of vanadium is 4-7 mu g/g.

The ore-rich precursor material 1 and the ore-rich precursor material 2 which are initially loaded into the reactor are reacted to become the V-rich material 1 and the vanadium-rich material 2, the V content of the V-rich material 1 and the V content of the vanadium-rich material 2 are respectively 51 mass percent and 42 mass percent after roasting analysis, and the V content is the refined high-value V₂O₅High quality material of (2).

Example 10

Raw materials:mixing raw materialsThe material was the same as in example 3.

A first reaction unit:similarly to example 3, except for the catalyst loading, in this example, the moving bed reactor of the first reaction unit was loaded with the ore-rich precursor material 1: RDM-33B residual oil demetalization and desulfurization transition catalyst is 50: 50 (V/V); the fixed bed reactor of the first reaction unit is filled with an ore-rich precursor material 2 and an RCS-31 desulfurization catalyst, and the filling volume ratio is as follows: ore-rich precursor material 2: RCS-31 ═ 45: 55.

the hydrotreating conditions were the same as in example 1.

Example 11

Raw materials:DOA, LCO and coal tar II (obtained from example 7) in example B were mixed according to the mass ratio of 15:5:5, the mixed raw materials were in a liquid state at room temperature, and the properties of the mixed raw materials are shown in Table 1.

A first reaction unit:the mixed raw materials were tested on a medium-sized moving bed-fixed bed heavy oil hydrotreater, the catalyst loading and process conditions were the same as those in example 1, and the product properties after hydrotreatment are shown in table 2.

A second reaction unit:the light component below 355 ℃ was tested in a fixed bed hydrocracking unit under the same catalyst and test conditions as in the light component below 335 ℃ hydrocracking test in example 1 to obtain a hydrocracked product with properties as shown in table 4.

Example 12

Raw materials:the mixed raw materials were the same as in example 3.

A first reaction unit:similar to example 3, except that in this example, the mixed feed was tested on a medium sized moving bed hydrotreater. The filling volume ratio of the rich-ore precursor material 1 and the RDM-33B residual oil demetallization and desulfurization transition catalyst in the moving bed reactor is as follows: rich-ore precursor material 1: RDM-33B ═50: 50. the process conditions were the same as in example 1, and the product properties after hydrotreatment are shown in Table 2.

Separation:the properties of the heavy components at 335 ℃ or higher in the liquid phase product obtained by fractional distillation of the hydrotreatment are shown in Table 3.

A second reaction unit:the light component below 335 ℃ was tested in a fixed bed hydrocracking unit using the same catalyst and test conditions as in the light component hydrocracking test of example 1 to obtain a hydrocracked product having the properties shown in table 4.

Example 13

Raw materials:the DOA and QY1 in example B were mixed at a mass ratio of 1:10, and the mixed raw materials were liquid at room temperature, and the properties of the mixed raw materials are shown in table 1.

A second reaction unit:the light component at a temperature of less than 350 ℃ is tested on a fixed bed hydrocracking unit, the catalyst and the test conditions are the same as those of the light component hydrocracking test in example 1, and the properties of the obtained hydrocracking product are shown in Table 4.

Example 14

Raw materials:the DOA and QY2 in example B were mixed at a mass ratio of 2:10, and the mixed raw materials were liquid at room temperature, and the properties of the mixed raw materials are shown in table 1.

A second reaction unit:is less thanThe light component at 335 ℃ was tested on a fixed bed hydrocracking unit under the same catalyst and test conditions as in the light component hydrocracking test in example 1 to obtain a hydrocracked product, the properties of which are shown in table 4.

Example 15

Raw materials:the mixed raw materials were the same as in example 1.

A first reaction unit:filling an ore-rich precursor material 1 in a moving bed reactor, filling the ore-rich precursor material 1, an RDM-33B residual oil demetalization desulfurization transition catalyst and an RCS-31 desulfurization catalyst in the fixed bed reactor according to the flow direction of reactants, wherein the filling volume ratio is as follows: rich precursor material 1 (moving bed reactor): rich precursor material 1 (fixed bed reactor): RDM-33B: RCS-31 ═ 30: 36: 14: 20.

the remaining conditions were the same as in example 1.

The product properties after hydrotreating of the mixed feed are shown in table 2.

The properties of the heavy components at 335 ℃ or higher in the liquid phase product obtained by fractional distillation of the hydrotreatment are shown in Table 3.

Example 16

Raw materials:the mixed raw materials were the same as in example 1.

A first reaction unit:the process is similar to that of example 1, except that in this example, according to the flowing direction of the reactants, the moving bed reactor of the first reaction unit is filled with the ore-rich precursor material 2, and the fixed bed reactor is filled with the ore-rich precursor material 1, the RDM-33B residual oil demetallization desulfurization transition catalyst, and the RCS-31 desulfurization catalyst, and the filling volume ratio is: ore-rich precursor material 2: rich-ore precursor material 1: RDM-33B: RCS-31 ═ 30: 36: 14: 20.

the remaining conditions were the same as in example 1.

The properties of the heavy components at 335 ℃ or higher in the liquid phase product obtained by fractionation and hydrotreatment are shown in Table 3.

Example 17

Raw materials:the mixed raw materials were the same as in example 1.

A first reaction unit:similar to example 1, except that the catalyst loading condition is different, in this example, according to the flowing direction of the reactants, the moving bed reactor of the first reaction unit is loaded with RDM-33B residual oil demetallization desulfurization transition catalyst, the fixed bed reactor is loaded with the protection catalysts RG-30B, RDM-33B residual oil demetallization desulfurization transition catalyst and RCS-31 desulfurization catalyst, and the loading volume ratio is as follows: RG-30B: RDM-33B: RCS-31 ═ 5: 20: 75.

the remaining conditions were the same as in example 1.

Example 18

Raw materials:the mixed raw materials were the same as in example 1.

A first reaction unit:similar to example 1, except that the catalyst loading condition is different, in this example, according to the reactant flow direction, the moving bed reactor of the first reaction unit is loaded with the ore-rich precursor material 2, and the fixed bed reactor is loaded with the ore-rich precursor material 3, the RDM-33B residual oil demetallization desulfurization transition catalyst, and the RCS-31 desulfurization catalyst, and the loading volume ratio is: ore-rich precursor material 2: mineral-rich precursor material 3: RDM-33B: RCS-31 ═ 30: 36: 14: 20.

the remaining conditions were the same as in example 1.

The product properties of the mixed feedstock after hydrotreating are shown in table 2.

Comparative example 1

Raw materials:by mixing DOA and QY3 in example B at a mass ratio of 3:10, DOA was not completely dissolved at 100 ℃, i.e., the resulting mixture was not liquid, and the properties of the raw materials for mixing are shown in Table 1.

Since the mixed raw materials contained a large amount of solids, the next test could not be carried out.

Table 1: mixed raw material properties

Table 2: product properties after heavy oil hydrotreating

Item	C₇Insoluble matter content by mass%	Carbon residue, mass%	Sulfur, mass%	Viscosity (100 ℃ C.), mm²/s	Ni+V,(μg/g)
						Example 1	0.4	3.1	0.19	3.0	4.9
Example 2	0.4	4.8	0.26	3.7	6.8
						Example 3	1.3	8.9	0.32	6.01	12.9
Example 4	1.6	9.9	0.35	17.9	22.6
						Example 5	0.5	6.4	0.28	5.2	5.8
Example 9	0.6	8.2	0.33	6.8	7.5
						Example 10	0.5	7.6	0.37	7.0	8.1
Example 11	1.1	8.6	0.61	7.9	8.5
						Example 12	2.1	9.8	0.70	8.5	9.0
Example 13	0.9	2.1	0.18	3.3	6.8
						Example 14	1.9	4.3	0.48	28.7	14.5
Example 15	0.5	3.6	0.33	5.1	6.1
						Example 16	0.45	3.4	0.31	5.0	5.9
Example 17	1.1	4.3	0.61	10.2	11.5
						Example 18	0.44	3.6	0.32	5.3	6.2

Table 3: heavy component properties

Table 4: hydrocracking gasoline product Properties

Item	The yield of the product is as follows,mass%	Density (20 ℃ C.), g/cm³	RON	Sulfur content, μ g/g
					Example 1	80.22	0.7122	95.5	5.3
Example 2	79.63	0.7233	92.8	6.1
					Example 3	80.64	0.7356	89.8	6.8
Example 4	77.93	0.7658	90.1	9.2
					Example 11	80.01	0.7214	95.1	5.4
Example 12	78.90	0.7310	95.0	5.9
					Example 13	77.5	0.7463	93.5	7.8
Example 14	78.5	0.7599	91.8	9.3
					Example 15	84.09	0.7284	95.5	7.0
Example 16	83.85	0.7310	95.25	6.5
					Example 17	84.87	0.7259	95.14	6.8
Example 18	83.93	0.7325	95.91	6.4

Table 5: properties of ore-rich precursor material

	Burn and reduce weight%	Specific surface area, m²/g	Water absorption, g/g
				Mineral-rich precursor material 1	13.5	263	1.08
Mineral-rich precursor material 2	29.9	279	1.22
				Mineral-rich precursor material 3	20.5	99	1.05

Table 6: properties of distillates rich in aromatic hydrocarbons

From the above results, it can be seen that the technology of the present invention is capable of producing high quality low sulfur marine fuel or low sulfur coke product feedstocks from DOA.

Moreover, the technology of the invention can obtain gasoline products with high quality and meeting national V standards.

The preferred embodiments of the present invention have been described above in detail, but the present invention is not limited thereto. Within the scope of the technical idea of the invention, many simple modifications can be made to the technical solution of the invention, including combinations of various technical features in any other suitable way, and these simple modifications and combinations should also be regarded as the disclosure of the invention, and all fall within the scope of the invention.

Claims

1. A process for hydroprocessing deoiled asphalt, comprising:

(1) introducing deoiled asphalt and an aromatic hydrocarbon-containing material flow into a first reaction unit for hydrogenation reaction, wherein the first reaction unit contains an ore-rich precursor material and/or a hydrogenation catalyst, the hydrogenation catalyst can catalyze at least one reaction selected from hydrodemetallization reaction, hydrodesulfurization reaction, hydrodeasphaltization reaction and hydrodecarbonization reaction, the first reaction unit is a moving bed-fixed bed hydrogenation combination unit or a moving bed hydrogenation unit, the dosage ratio of the deoiled asphalt and the aromatic hydrocarbon-containing material flow is that a mixed raw material formed by the deoiled asphalt and the aromatic hydrocarbon-containing material flow is in a liquid state at the temperature of not higher than 400 ℃, and the viscosity of the mixed raw material at the temperature of 100 ℃ is not higher than 400mm²S; the ore-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca and Mg;

(2) fractionating the liquid phase product from the first reaction unit to obtain a light component and a heavy component, wherein the cut points of the light component and the heavy component are 240-450 ℃;

(32) introducing the heavy components into a delayed coking unit for reaction to obtain at least one product selected from the group consisting of coker gasoline, coker diesel, coker gas oil and low sulfur petroleum coke; or as a low sulfur marine fuel oil component.

2. The process of claim 1, wherein in step (1), the deoiled asphalt and the aromatic hydrocarbon-containing stream are used in a ratio such that a viscosity at 100 ℃ of a mixed feedstock formed from the deoiled asphalt and the aromatic hydrocarbon-containing stream is not greater than 200mm²/s。

3. The process of claim 1, wherein in step (1), the deoiled bitumen and the aromatic hydrocarbon-containing stream are used in a ratio such that the 100 ℃ viscosity of the mixed feedstock formed from the deoiled bitumen and the aromatic hydrocarbon-containing stream is no greater than 100mm²/s。

4. The process according to any one of claims 1-3, wherein in step (1) the aromatic-containing stream is an aromatic-rich distillate and/or aromatic compounds.

5. The process as claimed in claim 4, wherein the end point of the aromatics-rich fraction is at 200 ℃ and 540 ℃ and the aromatics content is at least 20 wt.%.

6. The process of claim 5, wherein said aromatics-rich distillate has an aromatics content of 40 wt.% or greater.

7. The process of claim 5, wherein said aromatics-rich distillate has an aromatics content of 50 wt.% or greater.

8. The process of claim 4, wherein said aromatics-rich distillate is selected from at least one of LCO, HCO, ethylene tar, coal tar, coker gas oil, and coker gas oil.

9. The process according to claim 4, wherein the aromatic hydrocarbon compound is selected from benzene, toluene, xylene, naphthalene, a mixture of at least one C_1-6At least one of alkyl substituted naphthalene and aromatic hydrocarbon with more than three rings.

10. The process of claim 4, wherein in step (1), the aromatic-containing stream is an aromatic-rich distillate, and the mass ratio of the deoiled asphalt to the aromatic-containing stream is from 1:10 to 50: 10.

11. The process of claim 4, wherein in step (1), the aromatic-containing stream is an aromatic-rich distillate, and the mass ratio of the deoiled asphalt to the aromatic-containing stream is from 3:10 to 30: 10.

12. The process of claim 4, wherein in step (1), the aromatic hydrocarbon-containing stream is an aromatic hydrocarbon compound, and the mass ratio of the deoiled asphalt to the aromatic hydrocarbon compound is 1:10 to 50: 10.

13. The process of claim 4, wherein in step (1), the aromatic hydrocarbon-containing stream is an aromatic hydrocarbon compound, and the mass ratio of the amount of the deoiled asphalt to the aromatic hydrocarbon compound is 3:10 to 30: 10.

14. The method according to any one of claims 1 to 3, wherein in step (1), the deoiled asphalt is deoiled asphalt obtained by subjecting a heavy oil raw material to a solvent deasphalting treatment in a solvent deasphalting unit.

15. The process of claim 14, wherein the mass fraction of yield of the deoiled asphalt in the solvent deasphalting unit is not more than 50%.

16. The process of claim 14, wherein the mass fraction of yield of the deoiled asphalt in the solvent deasphalting unit is not more than 40%.

17. The process of claim 14, wherein the mass fraction of yield of the deoiled asphalt in the solvent deasphalting unit is not more than 30%.

18. The method of any of claims 1-3, wherein the method further comprises: recycling the coker diesel and/or coker wax obtained in step (32) back to step (1) as at least part of the aromatic-containing stream.

19. The process according to any one of claims 1 to 3, wherein in step (1), the operating conditions in the first reaction unit comprise: the reaction temperature is 280-450 ℃, the reaction pressure is 8.0-20.0 MPa, the volume ratio of hydrogen to oil is 400-2000, and the liquid hourly space velocity is 0.05-1.2 h^-1。

20. The process according to any one of claims 1 to 3, wherein in step (1), the operating conditions in the first reaction unit comprise: the reaction temperature is 330-420 ℃, the reaction pressure is 10.0-18.0 MPa, the volume ratio of hydrogen to oil is 600-1200, and the liquid hourly space velocity is 0.10-0.8 h^-1。

21. The method according to any one of claims 1 to 3, wherein, in step (1), the first reaction unit is a moving bed-fixed bed hydrogenation combination unit, and the moving bed is filled with a mineral-rich precursor material, and the fixed bed is sequentially filled with a mineral-rich precursor material and a hydrogenation catalyst or the fixed bed is filled with a hydrogenation catalyst.

22. The process of claim 21, wherein the ratio of the volume of the mineral-rich precursor material loaded in the moving bed to the sum of the volumes of the mineral-rich precursor material and the hydrogenation catalyst loaded in the fixed bed is from 10:90 to 60: 40.

23. The process of claim 21, wherein the ratio of the volume of the mineral-rich precursor material loaded in the moving bed to the sum of the volumes of the mineral-rich precursor material and the hydrogenation catalyst loaded in the fixed bed is from 20:80 to 40: 60.

24. The method of claim 21, wherein the method further comprises: and replacing the rich-ore precursor material filled in the moving bed with a fresh rich-ore precursor material in each period, wherein the replacement proportion accounts for 5-20 mass% of the total amount of the rich-ore precursor material filled in the moving bed.

25. The method of claim 21, wherein the method further comprises: and replacing the rich-ore precursor material filled in the moving bed with a fresh rich-ore precursor material in each period, wherein the replacement proportion accounts for 10-15 mass% of the total amount of the rich-ore precursor material filled in the moving bed.

26. The method of claim 21, wherein the method further comprises: and replacing the rich-ore precursor material filled in the moving bed with a fresh rich-ore precursor material in each period, wherein the period is 5-20 days.

27. The method of claim 21, wherein the method further comprises: and replacing the rich-ore precursor material filled in the moving bed with a fresh rich-ore precursor material in each period, wherein the period is 10-15 days.

28. The process according to any one of claims 1 to 3, wherein in step (1), the mineral-rich precursor material contains a carrier selected from at least one of aluminum hydroxide, alumina and silica, and an active component element supported on the carrier selected from at least one of group VIB and group VIII metal elements.

29. The method as claimed in claim 28, wherein, in step (1), the ore-rich precursor material has a scorch reduction of not less than 3 mass% and a specific surface area of not less than 80m²(ii) water absorption of not less than 0.9 g/g.

30. The method as recited in claim 28, wherein in step (1), the first reaction unit is sequentially charged with a first mineral-rich precursor material and a second mineral-rich precursor material, in terms of a reactant flow direction, and a ignition loss of the second mineral-rich precursor material is equal to or greater than that of the first mineral-rich precursor material.

31. The method of claim 30, wherein the first mineral-rich precursor material has a burn reduction of 3-15 mass% and the second mineral-rich precursor material has a burn reduction of no less than 15 mass%.

32. The method of claim 30, wherein the packing volume ratio of the first and second rich precursor materials is from 5:95 to 95: 5.

33. The process of any one of claims 1-3, wherein in step (31), the second reaction unit is a hydrocracking unit, and the operating conditions in the hydrocracking unit include: the reaction temperature is 330-420 ℃, the reaction pressure is 5.0-18.0 MPa, the volume ratio of hydrogen to oil is 500-2000, and the liquid hourly space velocity is 0.3-3.0 h^-1。

34. The process of claim 33, wherein the hydrocracking unit is packed with at least one hydrotreating catalyst and at least one hydrocracking catalyst.

35. The process according to any one of claims 1-3, wherein in step (31), the second reaction unit is a catalytic cracking unit and the catalytic cracking unit is a fluid catalytic cracking unit.

36. The process of claim 35, wherein the operating conditions in the fluidized catalytic cracking unit comprise: the reaction temperature is 500-600 ℃, the agent-oil ratio is 3-12, and the retention time is 1-10 s.

37. The process of claim 35, wherein the operating conditions of the fluidized catalytic cracking unit comprise: the reaction temperature is 520-580 ℃, the agent-oil ratio is 4-10, and the retention time is 2-5 s.

38. The method of any one of claims 1-3, wherein in step (31), the second reaction unit is a diesel hydro-upgrading unit and the operating conditions in the diesel hydro-upgrading unit include: the reaction temperature is 330-420 ℃, the reaction pressure is 5.0-18.0 MPa, the volume ratio of hydrogen to oil is 500-2000, and the liquid hourly space velocity is 0.3-3.0 h^-1。

39. The method of claim 38, wherein the diesel hydro-upgrading unit is loaded with at least one diesel hydro-upgrading catalyst.

40. The process of any one of claims 1-3, wherein in step (32), the heavy components are introduced into a delayed coking unit for reaction to yield at least one product selected from coker gasoline, coker diesel, coker gas oil, and low sulfur petroleum coke, and the operating conditions to the delayed coking unit comprise: the reaction temperature is 440-520 ℃, and the retention time is 0.1-4 h.

41. The process of any one of claims 1-3, wherein in step (32), the heavies are introduced to a delayed coking unit for reaction to produce low sulfur petroleum coke, and conditions are controlled such that the sulfur content of the heavies is no greater than 1.8 wt.%.

42. The process of claim 41, wherein in step (32), the heavies are introduced to a delayed coking unit for reaction to produce low sulfur petroleum coke and the conditions are controlled such that the low sulfur petroleum coke has a sulfur content of no greater than 3 wt.%.

43. The method of any one of claims 1-3 wherein in step (32) the heavy fraction is provided as a low sulfur bunker fuel oil fraction and conditions are controlled such that the sulfur content of the low sulfur bunker fuel oil fraction is no greater than 0.5 wt.%.

44. A system for hydroprocessing a deoiled asphalt, for performing the method of any one of claims 1-43, comprising:

45. The system of claim 44, wherein the delayed coking unit is in fluid communication with the first reaction unit for recycling the coker diesel and/or coker wax obtained in the delayed coking unit back into the first reaction unit.

46. The system of claim 44 or 45, further comprising a solvent deasphalting unit in fluid communication with said first reaction unit for introducing deasphalted oil obtained after solvent deasphalting of the heavy oil feedstock therein into said first reaction unit.