Hydrogenation treatment method and system for deoiled asphalt

Abstract

The present invention relates to the field of hydrocarbon oil processing and discloses a method and system for the hydrogenation treatment of de-oiled asphalt, wherein the method comprises: (2) introducing a de-oiled asphalt and an aromatic-containing stream into a first reaction unit for a hydrogenation reaction, wherein the first reaction unit comprises a mineral-rich precursor material and / or a hydrogenation catalyst, and the first reaction unit is a fixed-bed hydrogenation unit; (21) separating a liquid product from the first reaction unit to provide a first light component and a first heavy component; (31) introducing the first light component into a second reaction unit for reaction to provide a gasoline component, a diesel component and / or a BTX feedstock component; and (32) introducing the first heavy component into a delayed coking unit for reaction; or using the first heavy component as a low-sulfur marine fuel oil component. The treatment method provided in the present invention can realize high-value utilization of DOA.

Description

Technology Field

[0001] The present invention relates to the field of hydrocarbon oil processing, in particular to a method for hydrogenating deoiled asphalt and a system for hydrogenating deoiled asphalt. Background Technology

[0002] The high-efficiency conversion of residual oil is a core function for oil refining companies. Fixed-bed residual oil hydrogenation is a key technology for high-efficiency conversion and is characterized by superior product quality and mature methods.

[0003] However, the high content of asphaltenes and metals in the residual oil becomes a limiting factor in the operating time of the fixed-bed residual oil hydrogenation.

[0004] To address this problem, the Solvent Deasphalting (Demetallization) and Hydro-Catalytic Cracking (SHF) combined method for residue oil, developed by the SINOPEC Petroleum Processing Research Institute (RIPP), is an innovative technology that maximizes the production of clean automotive fuel from low-value vacuum residue oil and extends operating time. However, due to the high softening point of De-asphaltene (DOA), transportation and utilization are difficult, limiting the popularization of SHF technology.

[0005] A novel combined method for producing propylene-rich products by hydrogenation-deep catalytic cracking (DCC) of residual oil is limited by the influence of asphaltenes and metals in the residual oil. The hydrogen content of the hydrogenated residual oil is low, the hydrogenation operation time of the residual oil is short, the propylene yield from DCC is low, and the economic benefits of the combined technology are limited.

[0006] Also, in 2020, the sulfur fraction New low-sulfur marine fuel standard of 0.5 wt% and sulfur fraction A low-sulfur petroleum coke standard of 3.0 wt% is scheduled to be implemented. The technology to produce low-sulfur marine fuel (low-sulfur petroleum coke) at a low cost is also a task that needs to be urgently addressed at this time.

[0007] Therefore, converting DOA into a material for the production of low-sulfur marine fuel or low-sulfur petroleum coke is a technical challenge that needs to be solved. The problem to be solved

[0008] The objective of the present invention is to provide a method and system for hydrogenating de-oiled asphalt that overcomes the disadvantages of the prior art and enables the high-value utilization of DOA. means of solving the problem

[0009] To achieve the above objective, a first aspect of the present invention provides a method for hydrogenating deoiled asphalt comprising the following:

[0010] (2) a step of introducing a deoiled asphalt and an aromatic-containing stream into a first reaction unit for a hydrogenation reaction, wherein the first reaction unit comprises a mineral-rich precursor material and / or a hydrogenation catalyst, and the hydrogenation catalyst can catalyze at least one reaction selected from a hydrodemetallization reaction, a hydrodesulfurization reaction, a hydrodecarbonization reaction and a hydrodecarbonization reaction, and the first reaction unit is a fixed-bed hydrogenation unit, and the deoiled asphalt and aromatic-containing stream are used in a ratio such that the mixed feedstock formed by the deoiled asphalt and aromatic-containing stream becomes a liquid state at a temperature of 400°C or lower, and the mineral-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca and Mg;

[0011] (21) A step of separating the liquid product from the first reaction unit to provide a first light component and a first heavy component, wherein the cutting point of the first light component and the first heavy component is 240-450℃;

[0012] (31) A step of introducing a first light component into a second reaction unit for reaction to provide at least one product selected from a gasoline component, a diesel component and a BTX feedstock component, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit and a diesel hydrogenation upgrading unit; and

[0013] (32) introducing the first heavy component into a delayed coking unit for reaction to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil and low sulfur petroleum coke; or using the first heavy component as a component of low sulfur marine fuel oil.

[0014] The present invention also relates to a variation of the method of the first embodiment.

[0015] A second aspect of the present invention provides a hydrogenation treatment system for deoiled asphalt comprising the following:

[0016] A fixed-bed hydrogenation unit, a first reaction unit used to carry out a hydrogenation reaction of deoiled asphalt and an aromatic-containing stream;

[0017] A separation unit fluidly communicating with the first reaction unit for separating the liquid product from the first reaction unit;

[0018] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained from a separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;

[0019] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke;

[0020] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0021] The present invention also relates to a modification of a system of a second embodiment. Effects of the invention

[0022] According to the present invention, DOA and aromatic-containing streams are hydrogenated together by a fixed bed (e.g., hydrodesulfurization), and the hydrogenated first light component undergoes hydrocracking (RLG or RLA) to produce BTX and diesel fractions or catalytic cracking (LTAG) to produce gasoline fractions (and liquefied gas); and low-sulfur petroleum coke or heavy low-sulfur marine fuel is produced by the hydrogenated first heavy component.

[0023] The processing method provided by the present invention can realize high-value utilization of DOA. Brief explanation of the drawing

[0024] FIG. 1 is a flowchart of a de-oiled asphalt hydrogenation treatment method according to an embodiment of a first variation of the first aspect of the present invention. FIG. 2 is a flowchart of a de-oiled asphalt hydrogenation treatment method according to an embodiment of a second variation of the first aspect of the present invention. FIG. 3 is a flowchart of a de-oiled asphalt hydrogenation treatment method according to an embodiment of a third variation of the first aspect of the present invention. FIG. 4 is a flowchart of a de-oiled asphalt hydrogenation treatment method according to an embodiment of the fourth variation of the first aspect of the present invention. FIG. 5 is a flowchart of a de-oiled asphalt hydrogenation treatment method according to an embodiment of the fifth variation of the first aspect of the present invention. FIG. 6 is a flowchart of a de-oiled asphalt hydrogenation treatment method according to an embodiment of the sixth variation of the first aspect of the present invention. Specific details for implementing the invention

[0025] The endpoints and any values ​​of the ranges disclosed herein are not limited to exact ranges or values, and should be understood to include values ​​approximate to such ranges or values. In the case of numerical ranges, each range and each individual point value between the endpoint and the individual point value may be combined with one or more new numerical ranges, and such new numerical ranges should be interpreted as specifically disclosed herein.

[0026] In the present invention, code numbers such as (1), (2), (3), (31) indicating steps, code numbers such as first and second indicating various embodiments / variations, and the numbers of each reference numeral in the drawings are provided primarily to distinguish them from one another and, unless specifically stated otherwise, should not be interpreted as the order of steps or the order of combination of parts in the method. Furthermore, when referring to a (hydrogenation) reaction unit, since some exemplary embodiments of the reaction unit of the present invention are implemented by a hydrogenation reaction, for convenience, where the present invention relates to terms such as first and second reaction units, these terms may be used interchangeably with terms such as first and second hydrogenation units according to specific embodiments, and those skilled in the art will understand that they refer to the same purpose in these specific embodiments.

[0027] As mentioned above, a first aspect of the present invention provides a method for hydrogenating deoiled asphalt, and the method of the first aspect generally comprises the following:

[0028] (2) A step of introducing a deoiled asphalt and aromatic-containing stream into a first reaction unit for a hydrogenation reaction, wherein the deoiled asphalt and aromatic-containing stream are used in a ratio such that the mixed feedstock formed by the deoiled asphalt and aromatic-containing stream becomes liquid at a temperature of 400°C or lower;

[0029] (21) A step of fractionating the liquid product from the first reaction unit to provide a first light component and a first heavy component, wherein the cutting point of the first light component and the first heavy component is 240-450℃;

[0030] (31) A step of introducing a first light component into a second reaction unit for reaction to provide at least one product selected from a gasoline component, a diesel component and a BTX feedstock component, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit and a diesel hydrogenation upgrade unit; and

[0031] (32) introducing the first heavy component into a delayed coking unit for reaction to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil and low sulfur petroleum coke; or using the first heavy component as a component of low sulfur marine fuel oil.

[0032] The present invention also provides a plurality of embodiments and variations of the first aspect. In the context of the present invention, where embodiments and variations of the first, second, or other aspects of the invention are described for the same purpose, the description and / or definition of the various features used may apply to each aspect of the invention and each embodiment and its variations, unless other or more specific descriptions and / or definitions are provided for that aspect or for a specific embodiment or variation thereof.

[0033] Preferably, the deoiled asphalt and aromatic-containing streams are used in a ratio such that the mixed feedstock formed from the deoiled asphalt and aromatic-containing streams becomes liquid at a temperature of 280°C or lower. It is more preferable that the deoiled asphalt and aromatic-containing streams be used in a ratio such that the mixed feedstock formed from the deoiled asphalt and aromatic-containing streams becomes liquid at a temperature of 100°C or lower.

[0034] Particularly preferably, the first light component and the first heavy component have a cutting point of 350°C.

[0035] In one embodiment, in step (2), the hydrogenation reaction in the first reaction unit is carried out in the presence of a hydrogenation catalyst.

[0036] Preferably, in step (2), the deoiled asphalt and aromatic-containing stream is a mixed feedstock formed from the deoiled asphalt and aromatic-containing stream, with a viscosity of 400 mm at 100°C. 2 / s or less, more preferably 200 mm 2 / s or less, more preferably 100 mm 2 It is used as a ratio that makes it less than / s.

[0037] Preferably, in step (2), the aromatic-containing stream is an aromatic-rich fraction oil and / or an aromatic hydrocarbon compound.

[0038] Preferably, the aromatic-rich fraction oil has an endpoint of 200°C to 540°C and an aromatic content of 20% by weight or more, preferably 40% by weight or more, more preferably 50% by weight or more.

[0039] Preferably, the aromatic-rich fraction oil is at least one selected from LCO, HCO, ethylene tar, coal tar, coker diesel, and coker wax oil. The aromatic-rich fraction oil according to the present invention may be obtained from a method other than the method according to the present invention, or may be obtained from the method according to the present invention.

[0040] Preferably, the aromatic hydrocarbon is one or more selected from benzene, toluene, xylene, naphthalene, methylnaphthalene, branched naphthalene, and aromatic hydrocarbons having two or more rings, and preferably is a polycyclic aromatic hydrocarbon having three or fewer rings or a mixture thereof. Particularly preferably, the aromatic hydrocarbon is benzene, toluene, xylene, naphthalene, at least one C 1-6 It is at least one selected from the group consisting of naphthalene substituted with an alkyl group and three or more aromatic hydrocarbons.

[0041] According to a preferred embodiment, in step (2), the aromatic-containing stream is an aromatic-rich fractional oil, and the weight ratio of the de-oiled asphalt content to the aromatic-containing stream content is 1:10 to 50:10, more preferably 3:10 to 30:10.

[0042] According to another preferred embodiment, in step (2), the aromatic-containing stream is an aromatic hydrocarbon, and the weight ratio of degreased asphalt to aromatic hydrocarbon is 1:10 to 50:10; more preferably 3:10 to 20:10.

[0043] Preferably, in step (2), de-oiled asphalt is obtained by applying a heavy oil feedstock to a solvent de-asphalting method in a solvent deasphalting unit.

[0044] Preferably, in the solvent deasphalting unit, the yield of degreased asphalt is 50 weight% or less, more preferably 40 weight% or less, and even more preferably 30 weight% or less.

[0045] Preferably, the method of the present invention further comprises the step of recirculating the coker diesel and / or coker wax oil obtained in step (32) back to step (2) as at least part of the aromatic-containing stream.

[0046] Preferably, in step (2), the first reaction unit has: a reaction temperature of 280-450°C, a reaction pressure of 8.0-20.0 MPa, a hydrogen-to-oil volume ratio of 400-2000, and a liquid volume space velocity of 0.05-1.2 h -1 It is operated under the conditions of. More preferably, the first reaction unit is: a reaction temperature of 330-420°C, a reaction pressure of 10.0-18.0 MPa, a hydrogen-to-oil volume ratio of 600-1200, and a liquid volume space velocity of 0.10-0.8 h per hour. -1It is operated under the conditions of. The liquid volume space velocity and reaction pressure per hour are selected according to the characteristics of the material to be processed, the target conversion rate, and the purification depth.

[0047] Unless otherwise specified, all pressures described herein are gauge pressures.

[0048] The hydrogenation catalyst of the present invention may be a graded combination of different catalysts, and preferably, the hydrogenation catalyst may catalyze at least hydrogenation demetallation and hydrogenation desulfurization reactions.

[0049] According to the present invention, the specific type of catalyst capable of catalyzing the hydrogenation demetalization reaction, the hydrogenation desulfurization reaction, the hydrogenation deasphalting reaction, and the hydrogenation decarbonization reaction is not particularly limited, and any catalyst capable of catalyzing said reactions commonly used in the art may be used.

[0050] The hydrogenation catalyst of the present invention may be used, for example, with a porous refractory inorganic oxide as a support, an oxide or sulfide of a Group VIB and / or Group VIII metal as an active component, and optionally with an auxiliary agent added.

[0051] In one embodiment, the first reaction unit is a fixed-bed hydrogenation unit, a moving-bed-fixed-bed hydrogenation combination unit, or a moving-bed hydrogenation unit.

[0052] The present invention further provides a first variation of the technical solution of the first embodiment described below.

[0053] In the first variant, the first reaction unit comprises a hydrogenation catalyst and / or a mineral-rich precursor material capable of catalyzing at least one reaction selected from a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, a hydrogenation deasphalting reaction and a hydrogenation decarbonization reaction, wherein the mineral-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca, and Mg.

[0054] In one embodiment, the first reaction unit is a fixed-bed hydrogenation unit.

[0055] Preferably, in step (2), the mineral-rich precursor material comprises a support and an active component element loaded on the support, wherein the support is at least one selected from the group consisting of aluminum hydroxide, alumina, and silica, and the active component element is at least one metal element selected from the group consisting of Group VIB and Group VIII. More preferably, the active component of the mineral-rich precursor material is an oxide and / or sulfide of a metal element selected from Group VIB and Group VIII.

[0056] More preferably, in step (2), the mineral-rich precursor material has a loss on ignition of 3 weight% or more and a specific surface area of ​​80 m² 2 It has a weight of 0.9 g / g or more and a water absorption rate of 0.9 g / g or more. Loss on ignition refers to the percentage of reduced weight of the mineral-rich precursor material after roasting treatment at 600°C / 2h compared to the weight before roasting; water absorption rate refers to the percentage of increased weight of the mineral-rich precursor material after immersion in water at room temperature (e.g., 25°C) for 30 minutes compared to the weight before immersion.

[0057] According to a preferred embodiment, in step (2), the first reaction unit is sequentially filled with a mineral-rich first precursor material and a mineral-rich second precursor material along the flow direction of the reactants, wherein the mineral-rich second precursor material has a loss on ignition equal to or greater than that of the mineral-rich first precursor material.

[0058] According to the above preferred embodiment, the mineral-rich first precursor material has a loss on ignition of 3 to 15 weight%, and the mineral-rich second precursor material has a loss on ignition of 15 weight% or more.

[0059] According to the above preferred embodiment, it is more preferable that the mineral-rich first precursor material and the mineral-rich second precursor material are loaded in a volume ratio of 5:95 to 95:5.

[0060] Preferably, after the first reaction unit of the present invention has been operated for a long period, the mineral-rich precursor material is converted into a vanadium-rich material, and the vanadium content of the vanadium-rich material is 10 weight% or more.

[0061] A preferred embodiment of the first reaction unit of the present invention is provided below.

[0062] The hydrogenation technology of the feedstock related to the first reaction unit of the present invention is a fixed-bed hydrogenation technology. Taking conventional fixed-bed hydrogenation technology for heavy oil and residual oil as an example, the reactor or reaction bed comprises at least a mineral-rich precursor material and / or a hydrogenation catalyst. The mineral-rich precursor material consists of two parts: a support having a strong ability to adsorb vanadium-containing organic compounds in oil and an active component having a hydrogenation activity. The support is obtained by extruding, molding, and drying mainly silica, aluminum hydroxide, or a mixture of aluminum hydroxide and alumina. The surface of the support is rich in -OH groups. The support has a strong adsorption ability for vanadium-containing organic compounds in oil. The support has a loss on ignition of 5 wt% or more after roasting at 600°C for 2 hours. The active component mainly comprises oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, Ni, etc.

[0063] The hydrogenation catalyst associated with the aforementioned preferred embodiment is generally a heavy residue hydrogenation catalyst, and a heavy residue hydrogenation catalyst refers to a composite catalyst having functions such as heavy residue hydrogenation demetallation, hydrogenation desulfurization, and hydrogenation decarbonization. In the case of these catalysts, a porous refractory inorganic oxide such as alumina is generally used as a support, and oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, and Ni are used as active components, and various other auxiliary agents such as elements P, Si, F, and B, such as the RDM and RCS series heavy metals developed by RIPP, residue oil hydrogenation demetallation catalysts, and desulfurization catalysts are optionally added. Currently, multiple catalysts are often used together in fixed-bed residue oil hydrogenation technology. In the present invention, it is preferable to use a mineral-rich precursor material, a hydrogenation demetallation desulfurization catalyst, and a hydrogenation desulfurization catalyst, and these are generally loaded in a sequence such that the feedstock comes into sequential contact with the mineral-rich precursor material, the hydrogenation demetallation desulfurization catalyst, and the hydrogenation desulfurization catalyst. Of course, there is a technique for loading a mixture of these catalysts.

[0064] Preferably, in step (31), the second reaction unit has: a reaction temperature of 330-420°C, a reaction pressure of 5.0-18.0 MPa, a hydrogen-to-oil volume ratio of 500-2000, and a liquid volume space velocity of 0.3-3.0 h -1 It is a hydrocracking unit that operates under the conditions of

[0065] Preferably, at least one hydrogenation catalyst and at least one hydrocracking catalyst are loaded into the hydrocracking unit.

[0066] Preferably, the hydrocracking unit is a fixed-bed hydrocracking unit.

[0067] A preferred embodiment of the second reaction unit of the present invention is provided below.

[0068] In step (31), a first light component is introduced into a second reaction unit for reaction using a fixed-bed hydrocracking technique. Taking as an example a conventional technique in the industry for hydrocracking wax oil by a fixed bed, the reactor or reaction bed comprises at least two hydrocracking catalysts, namely a pretreatment catalyst and a hydrocracking catalyst. Since the material obtained by fractionation after fixed-bed hydrocracking has high metal, sulfur, and nitrogen content and a high carbon residue, it is desirable for the pretreatment catalyst to have strong demetallation activity and excellent desulfurization and denitrification activity to ensure subsequent hydrocracking catalyst activity. The hydrocracking catalyst preferably has excellent hydrocracking activity. In the case of such catalysts, porous refractory inorganic oxides such as alumina or molecular sieves are generally used as supports, oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, Ni, etc. are used as active components, and various other auxiliary agents such as elements P, Si, F, B, etc., such as the RS series pretreatment catalyst and RHC series hydrocracking catalyst developed by RIPP, are optionally added. The RS series catalyst is a NiW catalyst, and the RHC series catalyst is a NiMo molecular sieve catalyst.

[0069] Preferably, in step (31), the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluid catalytic decomposition (FCC) unit.

[0070] Preferably, the technology used for the catalytic cracking of the first light component is FCC technology, preferably LTAG technology developed by RIPP, which mainly produces gasoline fractions and liquefied gas.

[0071] Preferably, the fluid catalytic cracking unit is operated under conditions of: a reaction temperature of 500-600°C, a catalyst-to-oil ratio of 3-12, and a residence time of 1-10 seconds. More preferably, the fluid catalytic cracking unit is operated under conditions of: a reaction temperature of 520-580°C, a catalyst-to-oil ratio of 4-10, and a residence time of 2-5 seconds.

[0072] The catalyst-to-oil ratio of the present invention represents the weight ratio of catalyst to oil.

[0073] Preferably, in step (31), the second reaction unit is a diesel hydrogenation upgrade unit, with a reaction temperature of 330-420°C, a reaction pressure of 5.0-18.0 MPa, a hydrogen-to-oil volume ratio of 500-2000, and a liquid volume space velocity of 0.3-3.0 h -1 It operates under the conditions of.

[0074] Preferably, at least one diesel hydrogenation upgrade catalyst is loaded into the diesel hydrogenation upgrade unit.

[0075] Diesel hydrogenation upgrade catalysts may be composite catalysts having functions such as diesel hydrodesulfurization and hydrodenitrification. In the case of these catalysts, a porous refractory inorganic oxide such as alumina is generally used as a support, and oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, Ni, etc. are used as active components, and various other auxiliary agents such as elements P, Si, F, B, etc., such as the RS series heavy metals developed by RIPP, residual oil hydrodemetallization catalysts, and desulfurization catalysts are optionally added.

[0076] Preferably, in step (32), the first heavy component is introduced into a delayed coking unit for reaction to provide at least one product selected from coker gasoline, coker diesel, coker wax oil and low sulfur petroleum coke, wherein the delayed coking unit is operated under conditions of: a reaction temperature of 440-520°C and a residence time of 0.1-4 hours.

[0077] Preferably, in step (32), the sulfur content of the first heavy component is 1.8 weight% or less, and the first heavy component is introduced into a delayed coking unit for reaction to provide low-sulfur petroleum coke. More preferably, the conditions of the delayed coking unit are controlled so that the sulfur content of the low-sulfur petroleum coke is 3 weight% or less.

[0078] Preferably, in step (32), the first heavy component is used as a low-sulfur marine fuel oil component, and the sulfur content of the low-sulfur marine fuel oil component is 0.5 weight% or less.

[0079] According to the present invention, the specific operation for the solvent deasphalting treatment is not particularly limited, and conventional solvent deasphalting methods may be used. The operating parameters of the solvent deasphalting method are exemplified in the embodiments of the present invention and should not be understood by those skilled in the art as limiting the present invention.

[0080] The method of the present invention is suitable for the hydrogenation conversion of atmospheric pressure residue and vacuum residue, particularly for the hydrogenation conversion of poor residue oil that has a high metal content (Ni + V > 150 μg / g, especially Ni + V > 200 μg / g), a high carbon residue content (weight fraction of carbon residue > 17%, especially weight fraction of carbon residue > 20%), and a high content of fused cyclic materials.

[0081] In one embodiment, the hydrogenation catalyst can catalyze at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, a hydrogenation deasphalting reaction, and a hydrogenation decarbonization reaction, and the mineral-rich precursor material is a material capable of adsorbing at least one metal selected from the group consisting of V, Ni, Fe, Ca, and Mg.

[0082] An exemplary embodiment of a first variation of the technical solution of the first aspect can be seen in FIG. 1.

[0083] The hydrogenation treatment method of the first modified degreased asphalt is described in more detail below with reference to FIG. 1.

[0084] As illustrated in FIG. 1, a heavy oil feedstock (1) is supplied to a solvent deasphalting unit (2) to provide de-oiled asphalt (4) and deasphalted oil (3) through solvent deasphalting treatment; the de-oiled asphalt (4) and an aromatic-containing stream (5) are mixed to form a mixed feedstock (6), which is supplied to a first reaction unit (7) for a hydrogenation reaction, wherein the first reaction unit comprises a mineral-rich precursor material and / or a hydrogenation catalyst, and the first reaction unit is a fixed-bed hydrogenation unit; the liquid product from the first reaction unit (7) is supplied to a separation unit (19) for fractionation to provide a first light component (8) and a first heavy component (9); the first light component (8) is supplied to a second reaction unit (10) for reaction to provide at least one product selected from a gasoline component (13), a BTX feedstock component (12), and a diesel component (14); The first heavy component (9) is supplied to a delayed coking unit (11) for reaction to provide at least one product selected from the group consisting of coker gasoline (15), coker diesel (16), coker wax oil (17) and low-sulfur petroleum coke (18); or the first heavy component (9) is used as a low-sulfur marine fuel oil component.

[0085] Descriptions and / or definitions of features in a first variant of the technical solution of a first embodiment may be applied to various variants of the first embodiment of the invention as well as other embodiments and various variants thereof, unless there are different or more specific descriptions and / or definitions in other embodiments or various variants thereof. Similarly, descriptions and / or definitions of various features of various embodiments of the first embodiment of the invention as well as other various embodiments and various variants thereof (particularly features not specifically described and / or defined in such first variants) may be used in the first variant of the first embodiment, unless there are different or more specific descriptions and / or definitions in the first variant of the first embodiment.

[0086] The present invention further provides a second variation of the technical solution of the first embodiment described below.

[0087] In this second variation, the first reaction unit of the present invention is a moving-bed-fixed-bed hydrogenation bonding unit or a moving-bed hydrogenation unit. In a preferred first case, the first reaction unit is a moving-bed-fixed-bed hydrogenation bonding unit; in a preferred second embodiment, the first reaction unit is a moving-bed hydrogenation unit.

[0088] According to the present invention, the first reaction unit is particularly preferably a moving layer-fixed layer hydrogenation bonding unit.

[0089] According to a preferred embodiment, in step (2), the first reaction unit is a moving bed-fixed bed hydrogenation coupling unit, and a mineral-rich precursor material is loaded on the moving bed; a mineral-rich precursor material and a hydrogenation catalyst are sequentially loaded on the fixed bed, or a hydrogenation catalyst is loaded on the fixed bed.

[0090] Preferably, in step (2), the first reaction unit is a moving bed-fixed bed hydrogenation coupling unit, and a mineral-rich precursor material and a hydrogenation catalyst are sequentially loaded into the moving bed; a mineral-rich precursor material and a hydrogenation catalyst are sequentially loaded into the fixed bed, or a hydrogenation catalyst is loaded into the fixed bed.

[0091] In the above preferred embodiment, more preferably, the ratio of the volume of the mineral-rich precursor material loaded on the moving bed to the sum of the volumes of the mineral-rich precursor material and the hydrogenation catalyst loaded on the fixed bed is 10:90 to 60:40, preferably 20:80 to 40:60. When only the hydrogenation catalyst is loaded on the fixed bed, the loaded volume ratio should be described as representing the ratio of the volume of the mineral-rich precursor material loaded on the moving bed to the volume of the hydrogenation catalyst loaded on the fixed bed.

[0092] Preferably, the method of the present invention further comprises the step of replacing a mineral-rich precursor material loaded on a moving bed with a new mineral-rich precursor material at each period, wherein the replacement rate is 5-20% by weight, more preferably 10-15% by weight, relative to the total amount of mineral-rich precursor material loaded on the moving bed.

[0093] Preferably, the period is 5-20 days, preferably 10-15 days.

[0094] The mineral-rich precursor material of the present invention may be cylindrical and / or spherical, preferably spherical.

[0095] Preferably, the mineral-rich precursor material has an average particle size of 0.1 to 6 mm, more preferably 0.3 to 4 mm, and even more preferably 0.5 to 1.5 mm.

[0096] The new mineral-rich precursor material used to replace the mineral-rich precursor material loaded in the moving bed is in an oxidized or vulcanized state, preferably in a vulcanized state.

[0097] According to a preferred embodiment, in step (2), a mineral-rich first precursor material and a mineral-rich second precursor material are loaded sequentially into the first reaction unit according to the flow direction of the reactants, and the mineral-rich second precursor material has a loss on ignition equal to or greater than that of the mineral-rich first precursor material. According to the present invention, if conditions can be met in which the reactant first contacts the mineral-rich first precursor material and then contacts the mineral-rich second precursor material relative to the mineral-rich second precursor material, the specific loading locations of the mineral-rich first and second precursor materials are not particularly limited.

[0098] In this second variation, the feedstock hydrogenation technology associated with the first reaction unit of the present invention is a moving-bed-fixed-bed hydrogenation technology or a moving-bed hydrogenation technology. A moving-bed reactor is loaded with a spherical mineral-rich precursor material having an average particle size of 0.1-6 mm. The fixed-bed reaction bed comprises at least a mineral-rich precursor material and / or a hydrogenation catalyst, wherein the mineral-rich precursor material comprises two parts: one part which is a support having a strong ability to adsorb vanadium-containing organic compounds mainly in oil, and the other part which is an active component having a hydrogenation active function.

[0099] An exemplary embodiment of a second variation of the first aspect can be seen in FIG. 2.

[0100] Descriptions and / or definitions of features in a second variant of the technical solution of the first embodiment may be applied to various variants of the first embodiment of the invention as well as other embodiments and various variants thereof, unless there are different or more specific descriptions and / or definitions in other embodiments or various variants thereof. Similarly, descriptions and / or definitions of various features of various embodiments of the first embodiment of the invention as well as other various embodiments and various variants thereof (particularly features not specifically described and / or defined in these second variants) may be used in the second variant of the first embodiment, unless there are different or more specific descriptions and / or definitions in the second variant of the first embodiment.

[0101] The present invention further provides a third variation of the technical solution of the first embodiment described below.

[0102] According to this third variation, the method of the present invention further comprises the following:

[0103] (1) A step of introducing heavy raw oil into a solvent deasphalting unit for solvent deasphalting treatment to provide deasphalted asphalt and deasphalted oil;

[0104] (11) A step of introducing deasphalted oil into a third hydrogenation unit for a hydrogenation reaction, and introducing the liquid effluent obtained from the third hydrogenation unit into a DCC unit for a reaction to provide propylene, LCO, HCO and slurry oil, wherein the third hydrogenation unit is a fixed-bed hydrogenation unit;

[0105] (13) a step of introducing the slurry oil obtained from the DCC unit into a fourth hydrogenation unit for a demetalization reaction to provide a demetalization slurry oil; and

[0106] A step of using an aromatic-containing stream comprising a slurry obtained from a DCC unit and / or a demetallized slurry obtained from a fourth hydrogenation unit as an aromatic-containing stream (5) in step (2) of a first transformation or a second transformation, preferably the first transformation.

[0107] When the slurry oil obtained from the DCC unit and the de-asphalt obtained from the solvent deasphalting unit are introduced into the first hydrogenation unit for a conversion reaction, the slurry oil may or may not be filtered, preferably filtered, and the solid content is controlled to be ≤10 ppm.

[0108] Preferably, the aromatic-containing stream also comprises an aromatic-rich fraction oil, and the aromatic-rich fraction oil comprises LCO and / or HCO obtained from a DCC unit.

[0109] Preferably, in step (11), the operating conditions of the DCC unit are controlled so that the aromatic content of LCO and / or HCO is 60 weight% or more.

[0110] Preferably, the cutting point of LCO and HCO is 180-205°C; preferably, the cutting point of HCO and slurry oil is 330-360°C.

[0111] This third modification provides the following preferred embodiment for a solvent deasphalting unit:

[0112] Preferably, in step (1), the yield of de-oiled asphalt from the solvent deasphalting unit is 50 weight% or less, more preferably 40 weight% or less, and even more preferably 30 weight% or less.

[0113] Preferably, in step (1), the heavy crude oil is residual oil and / or heavy oil.

[0114] According to the third variation, the specific operation for the solvent deasphalting treatment is not particularly limited and may be carried out by a solvent deasphalting method commonly known in the art. This third variation does not list specific operation parameters for the solvent deasphalting method, and those skilled in the art should not be understood as limitations on this third variation.

[0115] This third variation provides the following preferred embodiment for the third hydrogenation unit.

[0116] Preferably, in step (11), the third hydrogenation unit has: a reaction temperature of 280-400°C, a reaction pressure of 6.0-14.0 MPa, a hydrogen-to-oil volume ratio of 600-1200, and a liquid space velocity of 0.3-2.0 h per hour. -1 It operates under the conditions of.

[0117] Preferably, in step (11), at least two hydrogenation catalysts are loaded into the third hydrogenation unit. More preferably, in step (11), the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction. The hydrogenation catalyst is generally supported on a porous refractory inorganic oxide such as alumina. Particularly preferably, in step (11), the hydrogenation catalyst comprises alumina as a support and a metal element of Group VIB and / or Group VIII as an active component element, and optionally also comprises at least one auxiliary element selected from P, Si, F, and B. In the hydrogenation catalyst, the metal element of Group VIB and Group VIII may be, for example, W, Mo, Co, Ni, etc. In the hydrogenation catalyst, the active component may be an oxide and / or sulfide of the aforementioned active component element.

[0118] A preferred embodiment of the third hydrogenation unit of this third variant is provided below:

[0119] The conditions of the third hydrogenation unit of deasphalted oil (DAO) in the presence of hydrogen are generally as follows: The hydrogenation technology of DAO is a fixed-bed hydrogenation technology. Taking currently industrialized fixed-bed heavy oil and residue oil hydrogenation technology as an example, the reactor or reaction bed contains at least two hydrogenation catalysts, and the heavy oil and residue oil hydrogenation catalysts refer to composite catalysts having functions such as hydrodemetallation, hydrodesulfurization, hydrodenitrification, and hydrodecarbonization for both heavy oil and residue oil. In the case of these catalysts, a porous refractory inorganic oxide such as alumina is generally used as a support, and oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, Ni, etc. are used as active components, and various other auxiliary agents such as elements P, Si, F, B, etc., such as the RDM, RCS series heavy metals developed by RIPP, residue oil hydrodemetallation catalysts, and desulfurization catalysts are optionally added. Currently, multiple catalysts are often used together in fixed-bed residue hydroprocessing technology. Hydrogenated demetallation, hydrogenated desulfurization, and hydrogenated denitrification catalysts are used in a typical loading sequence in which the raw oil comes into sequential contact with the hydrogenated demetallation, hydrogenated desulfurization, and hydrogenated denitrification catalysts, although sometimes one or two catalysts are absent depending on the situation. For example, only the hydrogenated demetallation and hydrogenated desulfurization catalysts are loaded, and the hydrogenated denitrification catalyst is not loaded. Of course, there are techniques for loading a mixture of these catalysts. The liquid space velocity and reaction pressure per hour are generally selected based on the properties of the material being processed, the target conversion rate, and the depth of purification.

[0120] This third variation provides the following preferred implementation for the second reaction unit.

[0121] Preferably, in step (31), the second reaction unit is a fixed-bed hydrocracking unit; preferably, at least two catalysts are loaded into the fixed-bed hydrocracking unit; the catalyst generally comprises a porous refractory inorganic oxide, such as alumina, as a support; preferably, the catalyst loaded into the fixed-bed hydrocracking unit comprises alumina as a support and a metal element of Group VIB and / or Group VIII as an active component element, and the catalyst optionally further comprises at least one auxiliary element selected from P, Si, F, and B. The metal element of Group VIB and Group VIII in the catalyst may be, for example, W, Mo, Co, Ni, etc. Additionally, the active component in the catalyst may be an oxide and / or sulfide of the aforementioned active component element. Particularly preferably, in step (31), the pretreated catalyst and the hydrocracking catalyst are sequentially loaded into the second reaction unit in the direction of the reactant flow.

[0122] Preferably, the second reaction unit is a fixed-bed hydrocracking unit, and the second reaction unit has: a reaction temperature of 330-420°C, a reaction pressure of 5.0-18.0 MPa, a hydrogen-to-oil volume ratio of 500-2000, and a liquid volume space velocity of 0.3-3.0 h -1 It is operated under the conditions of. More preferably, the second reaction unit is sequentially loaded with a pretreated catalyst and a hydrocracking catalyst in the direction of the reactant flow.

[0123] According to a preferred embodiment, in step (31), the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluidized catalytic decomposition unit.

[0124] This third variation provides the following preferred embodiment for the fourth hydrogenation unit.

[0125] Preferably, in step (13), the fourth hydrogenation unit is a fixed-bed hydrogenation unit, and the fourth hydrogenation unit has: a reaction temperature of 200-280°C, a reaction pressure of 3.0-6.0 MPa, a hydrogen-to-oil volume ratio of 600-1200, and a liquid space velocity of 0.5-2.5 h per hour. -1 It operates under the conditions of.

[0126] Preferably, in step (13), at least two hydrogenation catalysts are loaded into the fourth hydrogenation unit; more preferably, in step (13), the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction; the hydrogenation catalyst generally comprises a porous refractory inorganic oxide such as alumina as a support; particularly preferably, in step (13), the hydrogenation catalyst comprises alumina as a support and a metal element of Group VIB and / or Group VIII as an active component element, and the hydrogenation catalyst optionally further comprises at least one auxiliary element selected from P, Si, F and B. In step (13), the metal element of Group VIB and Group VIII in the hydrogenation catalyst may be, for example, W, Mo, Co, Ni, etc. In the hydrogenation catalyst, the active component may be an oxide and / or sulfide of the aforementioned active component element.

[0127] A preferred embodiment of the fourth hydrogenation unit of this third variant is provided below.

[0128] The hydrogenation technology for slurry oil is low-pressure fixed-bed hydrogenation technology. Taking currently industrialized fixed-bed heavy oil and residue oil hydrogenation technology as an example, the reactor or reaction bed contains at least two hydrogenation catalysts. The heavy oil and residue oil hydrogenation catalyst refers to a composite catalyst capable of converting heavy oil and residue oil into asphaltenes, as well as performing functions such as hydrodemetallation, hydrodesulfurization, hydrodenitrification, and hydrodecarbonization for both heavy oil and residue oil. In the case of these catalysts, porous refractory inorganic oxides such as alumina are generally used as supports, oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, and Ni are used as active components, and various other auxiliary agents such as elements P, Si, F, and B, such as the RDM and RCS series heavy metals developed by RIPP, residue oil hydrodemetallation catalysts, and desulfurization catalysts, are optionally added. Currently, multiple catalysts are often used together in fixed-bed residue oil hydrogenation technology. Hydrodemetallization catalysts, hydrodesulfurization catalysts, and hydrodenitrification catalysts are used in this general loading sequence in which crude oil comes into sequential contact with the hydrodemetallization catalyst, hydrodesulfurization catalyst, and hydrodenitrification catalyst, and sometimes one or two catalysts are absent depending on the situation. For example, only the hydrodemetallization catalyst and the hydrodesulfurization catalyst are loaded, and the hydrodenitrification catalyst is not loaded. Of course, there is a technique for loading a mixture of these catalysts. The liquid volume space velocity per hour and the reaction pressure are generally selected according to the properties of the material being processed, the target conversion rate, and the depth of purification.

[0129] A method for processing the heavy oil feedstock of the third modification is described in more detail below with reference to FIG. 3.

[0130] As illustrated in FIG. 1, a heavy oil feedstock (1) is supplied to a solvent deasphalting unit (2) for solvent deasphalting treatment to provide deasphalted asphalt (4) and deasphalted oil (3) through solvent deasphalting treatment; the deasphalted oil (3) is supplied to a third hydrogenation unit (29) for a hydrogenation reaction, and the liquid effluent (20) obtained from the third hydrogenation unit is supplied to a DCC unit (21) for reaction to provide propylene (22), LCO (23), HCO (24), and slurry oil (25); wherein the third hydrogenation unit is a fixed-bed hydrogenation unit; and the slurry oil (25) obtained from the DCC unit (21) is supplied to a fourth hydrogenation unit (26) for a demetalization reaction to provide demetalized slurry oil (27); A mixed feedstock (6) formed from an aromatic-containing stream together with de-oiled asphalt (4) obtained from a solvent deasphalting unit (2) is supplied to a first hydrogenation unit (7) for a conversion reaction, wherein the aromatic-containing stream comprises at least one selected from the group consisting of LCO (23) obtained from a DCC unit (21), HCO (24) obtained from a DCC unit (21), a demetallization slurry (27) obtained from a fourth hydrogenation unit (26), and an aromatic compound (5) from the outside, and the first hydrogenation unit is a fixed-bed hydrogenation unit or a moving-bed hydrogenation unit; The liquid effluent obtained from the first hydrogenation unit (7) is separated, and the first light component (8) obtained by separation is supplied to the second reaction unit (10) for reaction to provide at least one product selected from the group consisting of a gasoline component (13), a diesel component (14) and a BTX feedstock component (12), or at least a portion of the first light component (8) is recycled back to the DCC unit (21);The first heavy component (9) obtained by separation is fed to a delayed coking unit (11) for reaction to provide at least one product selected from the group consisting of coker gasoline (15), coker diesel (16), coker wax oil (17) and low-sulfur petroleum coke (18); or the first heavy component (9) is used as a low-sulfur marine fuel oil component.

[0131] Descriptions and / or definitions of features in a third variant of the technical solution of the first embodiment may be applied to various variants of the first embodiment of the invention as well as other embodiments and various variants thereof, unless there are different or more specific descriptions and / or definitions in other embodiments or various variants thereof. Similarly, descriptions and / or definitions of various features of various embodiments of the first embodiment of the invention as well as other various embodiments and various variants thereof (particularly features not specifically described and / or defined in these third variants) may be used in the third variant of the first embodiment, unless there are different or more specific descriptions and / or definitions in the third variant of the first embodiment.

[0132] The present invention further provides a fourth variation of the technical solution of the first embodiment described below.

[0133] The fourth variant is substantially similar to the third variant, but has the following main differences: LCO and / or HCO obtained from the DCC unit is incorporated into the aromatic-containing stream (5) in step (2), and the slurry oil (25) is recycled to the solvent deasphalting unit for solvent deasphalting without passing through the fourth hydrogenation unit in step (13).

[0134] When the first hard component is recirculated back to the DCC unit, the recirculation ratio is preferably 0.1 to 0.5:1.

[0135] The method for processing the heavy oil feedstock of the present invention is described in more detail below with reference to FIG. 4.

[0136] As illustrated in FIG. 4, heavy crude oil (1) is supplied to a solvent deasphalting unit (2) to provide deasphalted asphalt (4) and deasphalted oil (3) through solvent deasphalting treatment; the deasphalted oil (3) is supplied to a third hydrogenation unit (29) for a hydrogenation reaction, and the liquid effluent (20) obtained from the third hydrogenation unit is supplied to a DCC unit (21) for reaction to provide propylene (22), LCO (23), HCO (24) and slurry oil (25), wherein the third hydrogenation unit is a fixed-bed hydrogenation unit; LCO (23) and / or HCO (24) obtained from the DCC unit (21) and deasphalted pitch (4) obtained from the solvent deasphalting unit (2) are mixed to form a mixed feedstock (6), which is supplied to a first hydrogenation unit (7) for a conversion reaction, wherein the aromatic-containing stream is at least one selected from the group consisting of LCO (23) from the DCC unit (21), HCO (24) from the DCC unit (21), and aromatic hydrocarbons (5) from the outside, wherein the first hydrogenation unit (7) is a fixed-bed hydrogenation unit or a moving-bed hydrogenation unit; The liquid effluent obtained from the first hydrogenation unit (7) is separated, and the first light component (8) obtained by separation is supplied to the second reaction unit (10) for reaction to provide at least one product selected from the group consisting of a gasoline component (13), a diesel component (14) and a BTX feedstock component (12), or at least a portion of the first light component (8) is recycled back to the DCC unit (21); the first heavy component (9) is supplied to the delayed coking unit (11) for reaction to provide at least one product selected from the group consisting of coker gasoline (15), coker diesel (16), coker wax oil (17) and low-sulfur petroleum coke (18); or the first heavy component (9) is used as a low-sulfur marine fuel oil component.

[0137] Descriptions and / or definitions of features in a fourth variant of the technical solution of the first embodiment may be applied to various variants of the first embodiment of the invention as well as other embodiments and various variants thereof, unless there are different or more specific descriptions and / or definitions in other embodiments or various variants thereof. Similarly, descriptions and / or definitions of various features of various embodiments of the first embodiment of the invention as well as other various embodiments and various variants thereof (particularly features not specifically described and / or defined in such fourth variants) may be used in the fourth variant of the first embodiment, unless there are different or more specific descriptions and / or definitions in the fourth variant of the first embodiment.

[0138] The present invention further provides a fifth variation of the technical solution of the first embodiment described below.

[0139] The fifth variation includes the following:

[0140] Step (16): A step of introducing an aromatic-rich fraction into a fifth reaction unit for hydrosaturation and fractionating to provide a second light component and a second heavy component, wherein the second light component and the second heavy component have a cutting point of 100-250°C and the aromatic content in the second heavy component is 20% by weight or more; and

[0141] A step of incorporating a second heavy component into an aromatic-containing stream (5) in any one of the first to fourth variations, preferably in step (2) of the first variation.

[0142] Preferably, the hydrogenation saturation reaction performed in the fifth reaction unit of the fifth variant is partially hydrogenated, and particularly preferably, the second light component and the second heavy component have a cutting point of 180°C.

[0143] The second light component is preferably fed to a catalytic cracking unit to produce lower olefins.

[0144] Preferably, in step (16), the fifth reaction unit is at least one reactor among a fixed bed reactor, a moving bed reactor, and a boiling bed reactor.

[0145] Preferably, the fifth reaction unit has: a reaction temperature of 200-420°C, a reaction pressure of 2-18 MPa, and a liquid space velocity of 0.3-10 h per hour. -1 and is operated under conditions of a hydrogen-to-oil volume ratio of 50-5000. More preferably, the fifth reaction unit is: reaction temperature 220-400°C, reaction pressure 2-15 MPa, liquid space velocity 0.3-5 h per hour. -1 and is operated under conditions of a hydrogen-to-oil volume ratio of 50-4000.

[0146] A preferred embodiment of the fifth reaction unit of this fifth variation is provided below.

[0147] Partial hydrogenation saturation of aromatic-rich fractional oils in the presence of hydrogen is: generally, the partial hydrogenation saturation technology of aromatic-rich fractional oils is operated under conditions where the technology is a fixed-bed / boiling-bed / moving-bed hydrogenation technology. Taking currently industrialized fixed-bed diesel or wax oil hydrogenation technology as an example, the reactor or reaction bed contains at least one hydrofining catalyst. The hydrofining catalyst used for partial hydrogenation saturation of aromatic-rich fractional oils is desirable to have good and moderate hydrogenation saturation activity and additionally prevents the tetralin-like structure from being saturated with a decahydronaphthalene or cycloalkane structure having a lower hydrogen donating capacity. In the case of such catalysts, porous refractory inorganic oxides such as alumina or molecular sieves are generally used as supports, oxides or sulfides of Group VIB and / or Group VIII metals such as W, Mo, Co, Ni, etc. are used as active components, and various other auxiliary agents such as elements P, Si, F, B, etc., such as the RS series pretreatment catalyst developed by RIPP, are optionally added. The RS series catalyst is a NiMo catalyst.

[0148] The first reaction unit for the fifth variation is preferably an intermediate / low pressure fixed-bed hydrogenation unit.

[0149] Preferably, in step (2), the first reaction unit has: a reaction temperature of 260-500°C, a reaction pressure of 2.0-20.0 MPa, preferably 2-12 MPa, a hydrogen-to-oil volume ratio of 100-1200, and a liquid space velocity of 0.1-1.5 h -1 It is operated under the conditions of. The liquid volume space velocity and reaction pressure per hour are selected according to the properties of the material to be processed, the target conversion rate, and the purification depth.

[0150] A method for processing an aromatic-rich fraction oil according to the present invention is described in more detail below with reference to FIG. 5.

[0151] As illustrated in FIG. 5, the aromatic-rich fractionated oil (30) is supplied to the fifth reaction unit (31) for hydrogenation saturation and fractionated to provide a second light component and a second heavy component (32); the heavy oil feedstock (1) is supplied to the solvent deasphalting unit (2) for solvent deasphalting treatment to provide deasphalted asphalt (4) and deasphalted oil (3); An aromatic-containing stream comprising de-oiled asphalt (4) and a second heavy component (32) is mixed to form a mixed feedstock (6), which is supplied to a first reaction unit (7) for a hydrogenation reaction, wherein the aromatic-containing stream preferably also comprises an aromatic hydrocarbon (5) from the outside, wherein the first reaction unit comprises a hydrogenation catalyst capable of catalyzing at least one reaction selected from a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, a hydrogenation deasphalting reaction, and a hydrogenation decarbonization reaction, and a mineral-rich precursor material, and the first reaction unit is a fixed-bed hydrogenation unit; the liquid product from the first reaction unit (7) is supplied to a separation unit (19) for fractionation to provide a first light component (8) and a first heavy component (9), wherein the first light component and the first heavy component have a cutoff point of 240-450°C; A first light component (8) is supplied to a second reaction unit (10) for reaction to provide at least one product selected from a gasoline component (13), a BTX feedstock component (12), and a diesel component (14), wherein the second reaction unit is at least one selected from a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit; a first heavy component (9) is supplied to a delayed coking unit (11) for reaction to provide at least one product selected from the group consisting of coker gasoline (15), coker diesel (16), coker wax oil (17), and low-sulfur petroleum coke (18); or the first heavy component (9) is used as a low-sulfur marine fuel oil component.

[0152] Descriptions and / or definitions of features in the fifth variant of the technical solution of the first embodiment may be applied to various variants of the first embodiment of the invention as well as other embodiments and various variants thereof, unless there are different or more specific descriptions and / or definitions in other embodiments or various variants thereof. Similarly, descriptions and / or definitions of various features of various embodiments of the first embodiment of the invention as well as other various embodiments and various variants thereof (particularly features not specifically described and / or defined in these fifth variants) may be used in the fifth variant of the first embodiment, unless there are different or more specific descriptions and / or definitions in the fifth variant of the first embodiment.

[0153] The present invention further provides a sixth variation of the technical solution of the first embodiment described below.

[0154] The 6th variation includes the following:

[0155] (1) A step of introducing heavy crude oil into a solvent deasphalting unit for solvent deasphalting treatment to provide deasphalted asphalt and deasphalted oil;

[0156] (14) a step of introducing deasphalted oil into a sixth hydrogenation unit for a hydrogenation reaction, and introducing the liquid effluent obtained from the sixth hydrogenation unit into a DCC unit for a reaction to provide propylene, LCO, HCO and slurry oil, wherein the sixth hydrogenation unit is a fixed-bed hydrogenation unit; and

[0157] In step (16) of the fifth variation, LCO and / or HCO from the DCC unit is incorporated into an aromatic-rich fraction oil, or in step (16), LCO and / or HCO is used as an aromatic-rich fraction oil.

[0158] Accordingly, in one embodiment, step (1) of the sixth variation includes substantially the same features as described in step (1) of the third variation.

[0159] In addition, in one embodiment, the step (14) of the sixth variation includes substantially the same features as described in the step (11) of the third variation.

[0160] Preferably, the DCC unit of the 6th variant is operated under conditions of: a reaction temperature of 500-650°C, a catalyst-to-oil ratio of 3-12, and a residence time of 0.6-6 seconds.

[0161] In one embodiment, for the sixth variation, it is preferable that the LCO and HCO have a cutting point of 300 to 400°C; and the HCO and slurry oil have a cutting point of 400-500°C.

[0162] In one embodiment, the sixth variation further comprises: recirculating the coker diesel and / or coker wax oil obtained in step (32) to the fifth hydrogenation unit for hydrogenation saturation.

[0163] In one embodiment, at step (14) of this sixth variation, the sixth hydrogenation unit has: a reaction temperature of 280-400°C, a reaction pressure of 6.0-14.0 MPa, a hydrogen-to-oil volume ratio of 600-1200, and a liquid space velocity of 0.3-2.0 h per hour. -1 It operates under the conditions of.

[0164] In one embodiment, at step (14) of this sixth transformation, at least two hydrogenation catalysts are loaded into the sixth hydrogenation unit.

[0165] In one embodiment, in step (14) of the sixth modification, the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction and a hydrogenation decarbonization reaction.

[0166] In one embodiment, at step (14) of the sixth modification, the hydrogenation catalyst comprises alumina as a support and a metal element of group VIB and / or VIII as an active component element, and at least one auxiliary element optionally selected from P, Si, F and B.

[0167] A method for processing heavy crude oil and aromatic-rich fractional oil according to the 6th modified example is described in more detail below with reference to FIG. 6.

[0168] As illustrated in FIG. 1, a heavy oil feedstock (1) is supplied to a solvent deasphalting unit (2) for solvent deasphalting treatment to provide deasphalted asphalt (4) and deasphalted oil (3); the deasphalted oil (3) is supplied to a sixth hydrogenation unit (24) for a hydrogenation reaction, and the liquid effluent obtained from the sixth hydrogenation unit (24) is supplied to a DCC unit (35) for reaction to provide propylene (36), LCO (37), HCO (38) and slurry oil (33); an aromatic-rich fraction oil (30) containing LCO (37) and / or HCO (38) is supplied to a fifth hydrogenation unit (31) for hydrogenation saturation and fractionated to provide a second heavy component (32) and a second light component; A mixed feedstock (6) formed from an aromatic-containing stream comprising de-oiled asphalt (4) and a second heavy component (32) is supplied to a first reaction unit (7) for a hydrogenation reaction, wherein the aromatic-containing stream preferably also comprises an aromatic hydrocarbon (5) from the outside, and wherein the first reaction unit (7) comprises a hydrogenation catalyst and a mineral-rich precursor material capable of catalyzing at least one reaction selected from a hydrogenation demetalization reaction, a hydrogenation desulfurization reaction, a hydrogenation deasphalting reaction and a hydrogenation decarbonization reaction; and the liquid product from the first reaction unit (7) is supplied to a separation unit (19) for fractionation to provide a first light component (8) and a first heavy component (9); The first light component (8) is supplied to the second reaction unit (10) for reaction to provide at least one product selected from the group consisting of gasoline component (13), BTX feedstock component (12), and diesel component (14), or at least a portion of the first light component (8) is recycled back to the DCC unit (35); the first heavy component (9) is supplied to the delayed coking unit (11) for reaction to provide at least one product selected from the group consisting of coker gasoline (15), coker diesel (16), coker wax oil (17), and low-sulfur petroleum coke (18);Or the first heavy component (9) is used as a low-sulfur marine fuel oil component.;

[0169] Descriptions and / or definitions of features in the sixth variant of the technical solution of the first embodiment may be applied to various variants of the first embodiment of the invention as well as other embodiments and various variants thereof, unless there are different or more specific descriptions and / or definitions in other embodiments or various variants thereof. Similarly, descriptions and / or definitions of various features of various embodiments of the first embodiment of the invention as well as other various embodiments and various variants thereof (particularly features not specifically described and / or defined in these sixth variants) may be used in the sixth variant of the first embodiment, unless there are different or more specific descriptions and / or definitions in the sixth variant of the first embodiment.

[0170] As previously mentioned, a second aspect of the present invention provides a system for hydrogenating deoiled asphalt, and the system of a first variation of the second aspect comprises the following:

[0171] A fixed-bed hydrogenation unit, a first reaction unit used to carry out a hydrogenation reaction of deoiled asphalt and an aromatic-containing stream;

[0172] A separation unit fluidly communicating with the first reaction unit for separating the liquid product from the first reaction unit;

[0173] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained from a separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;

[0174] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke; and

[0175] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0176] Preferably, the delay coking unit fluidly communicates with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delay coking unit back to the first reaction unit.

[0177] Preferably, the system further comprises a solvent deasphalting unit, and the system further comprises a solvent deasphalting unit fluidly communicating with a first reaction unit, which is used to introduce de-asphalt obtained after solvent deasphalting treatment of a heavy oil feedstock into the first reaction unit.

[0178] According to a preferred embodiment, in the system of the present invention, the second reaction unit is a hydrocracking unit.

[0179] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluidized catalytic decomposition unit.

[0180] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a diesel hydrogenation upgrade unit.

[0181] The present invention further provides a second variation of the second embodiment described below.

[0182] In this second variant, the system includes the following:

[0183] A first reaction unit for carrying out a hydrogenation reaction of deoiled asphalt and an aromatic-containing stream, as a moving-bed-fixed-bed hydrogenation coupling unit or a moving-bed hydrogenation unit;

[0184] A separation unit fluidly communicating with the first reaction unit for separating the liquid product from the first reaction unit;

[0185] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained from a separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;

[0186] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke; and

[0187] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0188] Preferably, the delay coking unit fluidly communicates with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delay coking unit back to the first reaction unit.

[0189] Preferably, the system further comprises a solvent deasphalting unit, which fluidly communicates with the first reaction unit and is used to introduce de-oiled asphalt obtained after solvent deasphalting treatment of the heavy oil feedstock into the first reaction unit.

[0190] According to a preferred embodiment, in the system of the present invention, the second reaction unit is a hydrocracking unit.

[0191] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluidized catalytic decomposition unit.

[0192] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a diesel hydrogenation upgrade unit.

[0193] The present invention further provides a third variation of the second embodiment described below.

[0194] In the third variant, a solvent deasphalting unit used for the solvent deasphalting treatment of heavy crude oil to provide deasphalted asphalt and deasphalted oil;

[0195] A third hydrogenation unit fluidly communicating with a solvent deasphalting unit, wherein the third hydrogenation unit is a fixed-bed hydrogenation unit for hydrogenating the deasphalted oil from the solvent deasphalting unit;

[0196] A DCC unit fluidly communicating with a third hydrogenation unit for the reaction of the liquid effluent obtained from a third hydrogenation unit to provide propylene, LCO, HCO, and slurry oil;

[0197] A fourth hydrogenation unit fluidly communicating with a DCC unit to perform a demetalization reaction on the slurry oil obtained from a DCC unit in order to provide a demetalization slurry;

[0198] A first hydrogenation unit which is a fixed-bed hydrogenation unit or a moving-bed hydrogenation unit, wherein the first hydrogenation unit is in fluid communication with a DCC unit, a fourth hydrogenation unit, and a solvent deasphalting unit for a conversion reaction of de-oiled asphalt from a solvent deasphalting unit and demetallated slurry oil from a fourth hydrogenation unit and / or slurry oil from a DCC unit;

[0199] A separation unit capable of recirculating a first light component obtained from a separation unit back to a DCC unit and fluidly communicating with a first hydrogenation unit and a DCC unit, respectively, for separating a liquid effluent from a first hydrogenation unit;

[0200] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained from a separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;

[0201] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke; and

[0202] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0203] Preferably, the delayed coking unit fluidly communicates with the first hydrogenation unit to recirculate the coker diesel and / or coker wax oil obtained from the delayed coking unit back to the first hydrogenation unit.

[0204] The present invention further provides a fourth variation of the technical solution of the second embodiment described below.

[0205] In this fourth variant, the system includes the following:

[0206] A solvent deasphalting unit used for the solvent deasphalting treatment of heavy crude oil in a solvent deasphalting unit to provide deasphalted asphalt and deasphalted oil;

[0207] A third hydrogenation unit fluidly communicating with a solvent deasphalting unit, wherein the third hydrogenation unit is a fixed-bed hydrogenation unit for hydrogenating the deasphalted oil from the solvent deasphalting unit;

[0208] A DCC unit fluidly communicating with a third hydrogenation unit for the reaction of the liquid effluent obtained from a third hydrogenation unit to provide propylene, LCO, HCO, and slurry oil;

[0209] A first hydrogenation unit which is a fixed-bed hydrogenation unit or a moving-bed hydrogenation unit, wherein the first hydrogenation unit is in fluid communication with the DCC unit and the solvent deasphalting unit for the conversion reaction of deasphalted pitch from the solvent deasphalting unit and LCO and / or HCO from the DCC unit;

[0210] A separation unit capable of recirculating a first light component obtained from a separation unit back to a DCC unit and fluidly communicating with a first hydrogenation unit and a DCC unit, respectively, for separating a liquid effluent from a first hydrogenation unit;

[0211] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained in a separation unit, for providing at least one product selected from the group consisting of a gasoline fraction, a diesel fraction, and a BTX feedstock component;

[0212] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke; and

[0213] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0214] Preferably, the DCC unit fluidly communicates with the solvent deasphalting unit to recirculate the slurry obtained from the DCC unit for solvent deasphalting back to the solvent deasphalting unit.

[0215] The present invention provides a fifth variation of the technical solution of the second embodiment described below.

[0216] In this fifth variant, the system includes the following:

[0217] A fifth reaction unit for the hydrosaturation and fractionation of an aromatic-rich fraction oil to provide a second light component and a second heavy component;

[0218] A fixed-bed hydrogenation unit fluidly communicating with a fifth reaction unit, comprising a first reaction unit for the hydrogenation reaction of an aromatic-containing stream containing a second heavy component from the fifth reaction unit and deoiled asphalt;

[0219] A separation unit fluidly communicating with the first reaction unit for separating the liquid product from the first reaction unit;

[0220] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained from a separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;

[0221] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke; and

[0222] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0223] Preferably, the delay coking unit fluidly communicates with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delay coking unit back to the first reaction unit as at least part of the aromatic-containing stream.

[0224] Preferably, the system further comprises a solvent deasphalting unit, which is used to solvent deasphalt a heavy oil feedstock and to introduce the deasphalted asphalt obtained after solvent deasphalting into a first reaction unit and fluidly communicates with the first reaction unit.

[0225] According to a preferred embodiment, in the system of the present invention, the second reaction unit is a hydrocracking unit.

[0226] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluidized catalytic decomposition unit.

[0227] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a diesel hydrogenation upgrade unit.

[0228] The present invention further provides a sixth variation of the technical solution of the second embodiment described below.

[0229] In this sixth variation, the system includes the following.

[0230] A solvent deasphalting unit used for the solvent deasphalting treatment of heavy crude oil in a solvent deasphalting unit to provide deasphalted asphalt and deasphalted oil;

[0231] A sixth hydrogenation unit fluidly communicating with a solvent deasphalting unit, wherein the sixth hydrogenation unit is a fixed-bed hydrogenation unit for the hydrogenation reaction of deasphalted oil from the solvent deasphalting unit;

[0232] A DCC unit fluidly communicating with the 6th hydrogenation unit for the reaction of the liquid effluent obtained from the 6th hydrogenation unit to provide propylene, LCO, HCO, and slurry oil;

[0233] A fifth hydrogenation unit fluidly communicating with a DCC unit for hydrogenating and fractionating an aromatic-rich fraction oil containing LCO and / or HCO to provide a second light component and a second heavy component;

[0234] A first reaction unit, which is a fixed-bed hydrogenation unit fluidly communicating with a fifth hydrogenation unit and a solvent deasphalting unit, for a hydrogenation reaction of an aromatic-containing stream comprising deasphalted pitch from a solvent deasphalting unit and a second heavy component from a fifth hydrogenation unit;

[0235] A separation unit capable of recirculating a first light component obtained from a separation unit back to a DCC unit and fluidly communicating with a first reaction unit and a DCC unit, respectively, for fractionating a liquid product from a first reaction unit;

[0236] A second reaction unit fluidly communicating with a separation unit for the reaction of a first light component obtained from a separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;

[0237] A delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke; and

[0238] An outlet fluidly communicating with a separation unit for releasing a first heavy component obtained from a separation unit into a low-sulfur marine fuel oil fraction from the system.

[0239] Preferably, the delayed coking unit fluidly communicates with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delayed coking unit back to the fifth hydrogenation unit.

[0240] According to a preferred embodiment, in the system of the present invention, the second reaction unit is a hydrocracking unit.

[0241] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluidized catalytic decomposition unit.

[0242] According to another preferred embodiment, in the system of the present invention, the second reaction unit is a diesel hydrogenation upgrade unit.

[0243] Using a preferred embodiment of the present invention, compared with the prior art, the present invention adopts an effective combination of methods such as solvent deasphalting, heavy oil hydrogenation, hydrocracking, catalytic cracking, or coking to utilize light petroleum fractions with high efficiency, as well as to realize high efficiency, environmental protection, and comprehensive utilization of heavy petroleum resources through the conversion of low-value DOA low-sulfur marine fuel components and low-sulfur petroleum coke feedstocks that meet environmental protection requirements.

[0244] The present invention is described in detail by the following examples. Unless otherwise specified, the following examples were performed using the method flow illustrated in FIG. 1.

[0245] The results in Table 2 of the following examples are the average of the results obtained from sampling tests every 25 hours by operating the device continuously for 100 hours, unless specifically stated otherwise.

[0246] Catalytic decomposition catalyst MLC-500, RS-2100 hydrogenation purification catalyst, RHC-131 hydrocracking catalyst, RG-30B, RDM-33B, and RCS-31 are all catalysts produced by SINOPEC CATALYST CO.,LTD. CHANGLING DIVISION.

[0247] The characteristics of the aromatic-rich fraction oils used in each example are presented in Table 6.

[0248] The normal temperature below is 25±3℃.

[0249] Example IA

[0250] Preparation of Mineral-Rich Precursor Material 1: 2000g of RPB110 pseudoboehmite produced by SINOPEC CATALYST CO.LTD CHANGLING DIVISION was used. 1000g was treated at 550°C for 2 hours to yield approximately 700g of alumina. The approximately 700g of alumina and the remaining 1000g of pseudoboehmite were thoroughly mixed. To this, 40g of sesbania powder and 20g of citric acid were added, followed by the addition of 2200g of deionized water. The mixture was then kneaded, extruded into a strip, and dried at 300°C for 3 hours to produce a support of approximately 1730g. For saturation impregnation, 2100mL of a solution containing Mo and Ni was added, wherein the Mo content in the solution is A mineral-rich precursor material 1 was obtained by impregnating the material for 30 minutes with a content of 5.5 wt% calculated as MoO3 and 1.5 wt% calculated as NiO, and then treating it at 180°C for 4 hours, and its characteristics are presented in Table I-5.

[0251] Preparation of Mineral-Rich Precursor Material 2: 2000g of RPB110 pseudoboehmite produced by SINOPEC CATALYST CO.LTD CHANGLING DIVISION was used. To this, 30g of sesbania powder and 30g of citric acid were added, along with 2400g of deionized water. The mixture was kneaded, extruded into a strip, and dried at 120°C for 5 hours to produce a support of approximately 2040g. For saturation impregnation, 2200mL of a solution containing Mo and Ni was added. The Mo content in the solution was calculated as 7.5 wt% (MoO3), and the Ni content was calculated as 1.7 wt% (NiO). After impregnation for 30 minutes, the material was treated at 200°C for 3 hours to obtain Mineral-Rich Precursor Material 2, the characteristics of which are shown in Table I-5. presented.

[0252] Preparation of mineral-rich precursor material 3: 2000g of commercially available silica was used, 30g of sesbania powder and 30g of sodium hydroxide were added to it, and 2400g of deionized water was added. The mixture was kneaded, extruded into a strip, and dried at 120°C for 5 hours to prepare a support. For saturation impregnation, 2200mL of a solution containing Mo and Ni was added to it, wherein the Mo content in the solution was 4.5 wt% calculated as MoO3 and the Ni content was 1.0 wt% calculated as NiO. After impregnation for 30 minutes, the material was treated at 200°C for 3 hours to obtain mineral-rich precursor material 3, the characteristics of which are presented in Table I-5.

[0253] Example IB

[0254] Solvent deasphalting was performed using vacuum residue from the Middle East as a feedstock, and the solvent was a hydrocarbon mixture containing mainly butane (butane content 75 wt%) and small amounts of propane and pentane, wherein solvent deasphalting was performed at 120°C with a solvent:vacuum residue ratio of 1.5:1 (weight ratio) to obtain a yield of 68.1 wt% deasphalted oil (DAO) and 31.9 wt% de-oiled asphalt (DOA).

[0255] Example I-1

[0256] Feedstock: The DOA of Example 1-B was mixed with LCO in a weight ratio of 1:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0257] 1st reaction unit: The mixed feedstock was tested in a medium-scaled fixed-bed heavy oil hydrotreatment unit. Depending on the flow direction of the reactants, RG-30B protective catalyst, mineral-rich precursor material 1, mineral-rich precursor material 2, RDM-33B residue demetallation and desulfurization transfer catalyst, and RCS-31 desulfurization catalyst were sequentially loaded into the reactor of the first reaction unit in the following loading volume ratios: RG-30B: mineral-rich precursor material 1: mineral-rich precursor material 2: RDM-33B: RCS-31 = 6: 30: 30: 14: 20. The fixed-bed heavy oil hydrotreatment was performed at: temperature 380°C, reaction pressure 16 MPa, and liquid volume space velocity 0.18 h -1 , operated under conditions of a hydrogen / oil ratio (by volume) of 1000:1. After fixed-bed hydrogenation treatment of the mixed feedstock, the characteristics of the product are presented in Table I-2.

[0258] separation: The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table I-3.

[0259] 2nd Reaction Unit: Hydrocracking tests were performed on the first light component in a fixed-bed hydrocracking apparatus at a temperature below 335°C, and the catalyst loading ratios were as follows: RS-2100: RHC-131 = 40:60 (V / V). The hydrocracking method was: purification section temperature 370°C, cracking section temperature 385°C, reaction pressure 7 MPa, liquid volume space velocity 2.0 h -1 and operated under conditions of a hydrogen / oil volume ratio of 1200:1. The characteristics of the obtained hydrocracking gasoline products are presented in Table I-4.

[0260] Example I-2

[0261] Feedstock: The DOA of Example 1-B was mixed with HCO in a weight ratio of 5:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0262] The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrogenation treatment of Example I-1, and the characteristics of the product after hydrogenation treatment are presented in Table I-2.

[0263] separation: The liquid product obtained from the hydrogenation of fixed-bed residue oil was fractionated, and the characteristics of the first heavy component at a temperature of 378°C or higher were presented in Table I-3.

[0264] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 378°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 335°C in Example I-1, and the hydrocracking products were obtained and their characteristics are presented in Table I-4.

[0265] Example I-3

[0266] Feedstock: The DOA of Example 1-B was mixed with LCO in a weight ratio of 10:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0267] 1st reaction unit: The mixed feedstock was tested in a medium-sized fixed-bed heavy oil hydrotreatment apparatus. The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrotreatment of Example I-1, and the characteristics of the product after hydrotreatment are presented in Table I-2.

[0268] separation: The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table I-3.

[0269] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 335°C in Example I-1, and the hydrocracking products were obtained and their characteristics are presented in Table I-4.

[0270] Example I-4

[0271] Feedstock: The DOA of Example 1-B was mixed with coal tar in a weight ratio of 15:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0272] 1st reaction unit: The mixed feedstock was tested in a medium-sized fixed-bed heavy oil hydrotreatment apparatus. The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrotreatment of Example I-1, and the characteristics of the product after hydrotreatment are presented in Table I-2.

[0273] separation: The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 355°C or higher were presented in Table I-3.

[0274] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 355°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 335°C in Example I-1, and the hydrocracking products were obtained and their characteristics are presented in Table I-4.

[0275] Example I-5

[0276] A method similar to Example I-3 was used, except for the following:

[0277] 1st reaction unit: In this embodiment, the temperature of the fixed-bed heavy oil hydrotreatment was 395°C. Depending on the flow direction of the reactants, the RG-30B protective catalyst, mineral-rich precursor material 1, and RCS-31 desulfurization catalyst were loaded into the reactor of the first reaction unit in the following volume loading ratios: RG-30B: mineral-rich precursor material 1: RCS-31 = 7: 65: 28.

[0278] Other conditions were the same as in Example I-3.

[0279] The main physicochemical properties of the first heavy component obtained at a temperature above 350℃ are presented in Table I-3.

[0280] Example I-6

[0281] The DOA of Example 1-B was mixed with LCO in a weight ratio of 10:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0282] The catalyst loading and fixed-bed heavy oil hydrogenation treatment conditions were the same as in Example I-3.

[0283] The reaction temperature of the fixed bed was increased by 3°C every 30 days, and the operation was stopped after 300 days of operation of the hydrogenation test. The oil produced by hydrogenation had a sulfur weight fraction of 0.46 to 0.50% and a vanadium content of 10 to 15 μg / g.

[0284] Mineral-rich precursor material 1 and mineral-rich precursor material 2, initially loaded into the reactor, became V-rich material 1 and V-rich material 2, with V content of 55 wt% and 45 wt%, respectively, by roasting analysis after reaction, and are high-quality materials capable of producing high-value V2O5.

[0285] Example I-7

[0286] From Example I-3, a first heavy component was supplied to a delayed coking unit for coking treatment at a temperature of 350°C or higher, and the delayed coking unit was operated under conditions of: a reaction temperature of 490°C and a residence time of 1.5 hours.

[0287] Low-sulfur petroleum coke was obtained with a yield of 28.7% by weight, and the sulfur weight fraction in the petroleum coke was 2.7%.

[0288] Example I-8

[0289] A catalytic decomposition test was performed on the first light component obtained in Example I-3 at a temperature of less than 350°C using a small-scaled catalytic decomposition fixed fluidized bed test apparatus, wherein the catalyst was the catalytic decomposition catalyst MLC-500; and the fluidization catalyst unit was operated under conditions of a reaction temperature of 540°C, a catalyst-to-oil ratio of 6, and a residence time of 3 seconds.

[0290] As a result, the product gasoline was obtained in a yield of 55.2 wt%, and the RON octane rating of the gasoline was 95.8.

[0291] Example I-9

[0292] Feedstock: The mixed feedstock was the same as in Example I-3.

[0293] 1st reaction unit: Except for the difference in catalyst loading, it was similar to Example I-3. In this example, RG-30B: mineral-rich precursor material 1: mineral-rich precursor material 2 = 5: 60: 35 (V / V) were loaded sequentially according to the flow direction of the reactants. The fixed-bed heavy oil hydrotreatment conditions were the same as in Example I-3.

[0294] The reaction temperature of the fixed bed was increased by 3°C every 30 days, and the operation was stopped after 330 days of operation of the hydrogenation test. The oil produced by hydrogenation had a sulfur weight fraction of 0.55–0.65% and a vanadium content of 4–7 μg / g.

[0295] Mineral-rich precursor material 1 and mineral-rich precursor material 2, initially loaded into the reactor, became V-rich material 1 and V-rich material 2, with V content of 58 wt% and 47 wt%, respectively, by roasting analysis after reaction, and are high-quality materials capable of producing high-value V2O5.

[0296] Example I-10

[0297] Feedstock: The mixed feedstock was the same as in Example I-3.

[0298] 1st reaction unit: Except for the difference in catalyst loading, it was similar to Example I-3. In this example, RG-30B: mineral-rich precursor material 1 = 10: 90 (V / V) were loaded sequentially according to the flow direction of the reactants. The fixed-bed heavy oil hydrotreatment conditions were the same as in Example I-3.

[0299] The reaction temperature of the fixed bed was increased by 3°C every 30 days, and the operation was stopped after 300 days of operation of the hydrogenation test. The oil produced by hydrogenation had a sulfur weight fraction of 0.56–0.68% and a vanadium content of 2–4 μg / g.

[0300] Mineral-rich precursor material 1 initially loaded into the reactor became V-rich material 1 with a V content of 61 wt% by roasting analysis, which is a high-quality material capable of producing high-value V2O5.

[0301] Example I-11

[0302] Feedstock: The DOA of Example 1-B was mixed with LCO and coal tar II (obtained in Example I-7) in a weight ratio of 15:5:5, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0303] 1st reaction unit: The mixed feedstock was tested in a medium-sized fixed-bed heavy oil hydrotreatment apparatus. The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrotreatment of Example I-1, and the characteristics of the product after hydrotreatment are presented in Table I-2.

[0304] separation: The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 355°C or higher were presented in Table I-3.

[0305] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 355°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 335°C in Example I-1, and the hydrocracking products were obtained and their characteristics are presented in Table I-4.

[0306] Example I-12

[0307] Feedstock: The DOA of Example IB was mixed with QY1 in a weight ratio of 1:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0308] 1st reaction unit: The mixed feedstock was tested in a medium-sized fixed-bed heavy oil hydrotreatment apparatus. The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrotreatment of Example I-1, and the characteristics of the product after hydrotreatment are presented in Table I-2.

[0309] separation: The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table I-3.

[0310] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 335°C in Example I-1, and the hydrocracking products were obtained and their characteristics are presented in Table I-4.

[0311] Example I-13

[0312] Feedstock: The DOA of Example IB was mixed with QY2 in a weight ratio of 2:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table I-1.

[0313] 1st reaction unit: The mixed feedstock was tested in a medium-sized fixed-bed heavy oil hydrotreatment apparatus. The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrotreatment of Example I-1, and the characteristics of the product after hydrotreatment are presented in Table I-2.

[0314] separation: The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table I-3.

[0315] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 335°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 335°C in Example I-1, and the hydrocracking products were obtained and their characteristics are presented in Table I-4.

[0316] Example I-14

[0317] Feedstock: The mixed feedstock was the same as in Example I-1.

[0318] 1st reaction unit: Except for the difference in catalyst loading, this example was similar to Example I-1. In this example, according to the flow direction of the reactants, RG-30B protective catalyst, mineral-rich precursor material 1, RDM-33B residual oil demetallation and desulfurization transfer catalyst, and RCS-31 desulfurization catalyst were sequentially loaded into the reactor of the first reaction unit in the following loading volume ratios: RG-30B: mineral-rich precursor material 1: RDM-33B: RCS-31 = 6: 60: 14: 20.

[0319] Other conditions were the same as in Example I-1.

[0320] The characteristics of the product after fixed-bed hydrogenation treatment of the mixed feedstock are presented in Table I-2.

[0321] The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table I-3.

[0322] Example I-15

[0323] Feedstock: The mixed feedstock was the same as in Example I-1.

[0324] 1st reaction unit: It was similar to Example I-1, except that the catalyst loading was different. In this example, depending on the flow direction of the reactants, mineral-rich precursor material 2 was loaded first, followed by mineral-rich precursor material 1, into the reactor of the first reaction unit, i.e.:

[0325] Depending on the flow direction of the reactants, RG-30B protective catalyst, mineral-rich precursor material 2, mineral-rich precursor material 1, RDM-33B residue oil demetallation and desulfurization transfer catalyst, and RCS-31 desulfurization catalyst were loaded into the reactor of the first reaction unit in the following loading volume ratios: RG-30B: mineral-rich precursor material 2: mineral-rich precursor material 1: RDM-33B: RCS-31 = 6: 30: 30: 14: 20.

[0326] Other conditions were the same as in Example I-1.

[0327] The characteristics of the product after fixed-bed hydrogenation treatment of the mixed feedstock are presented in Table I-2.

[0328] The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table I-3.

[0329] Example I-16

[0330] Feedstock: The mixed feedstock was the same as in Example I-1.

[0331] 1st reaction unit: It was similar to Example I-1, except that the catalyst loading was different. In this example, according to the flow direction of the reactants, the RG-30B protective catalyst, the RDM-33B residue oil demetallation and desulfurization transfer catalyst, and the RCS-31 desulfurization catalyst were sequentially loaded into the reactor of the first reaction unit in the following loading volume ratios: RG-30B: RDM-33B: RCS-31 = 10: 40: 50.

[0332] Other conditions were the same as in Example I-1.

[0333] The characteristics of the product after fixed-bed hydrogenation treatment of the mixed feedstock are presented in Table I-2.

[0334] The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table I-3.

[0335] Example I-17

[0336] Feedstock: The mixed feedstock was the same as in Example I-1.

[0337] 1st reaction unit: Except for the difference in catalyst loading, this example was similar to Example I-1. In this example, according to the flow direction of the reactants, RG-30B protective catalyst, mineral-rich precursor material 3, mineral-rich precursor material 2, RDM-33B residual oil demetallation and desulfurization transfer catalyst, and RCS-31 desulfurization catalyst were sequentially loaded into the reactor of the first reaction unit in the following loading volume ratios: RG-30B: mineral-rich precursor material 3: mineral-rich precursor material 2: RDM-33B: RCS-31 = 6: 30: 30: 14: 20.

[0338] Other conditions were the same as in Example I-1.

[0339] The characteristics of the product after fixed-bed hydrogenation treatment of the mixed feedstock are presented in Table I-2.

[0340] The liquid product obtained from the fixed-bed heavy oil hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table I-3.

[0341] Comparative Example I-1

[0342] Feedstock: DOA of Example IB was mixed with QY3 in a weight ratio of 3:10, and DOA could not be completely dissolved at 100°C, that is, the obtained mixture was not a liquid, and the characteristics of the mixed feedstock are presented in Table I-1.

[0343] The mixed feedstock contained a large amount of solids, so the subsequent experiment could not be performed.

[0344] Table I-1: Characteristics of Mixed Feedstocks

[0345]

[0346] Table I-2: Characteristics of products after fixed-bed heavy oil hydrogenation

[0347]

[0348] Table I-3: Characteristics of the First Heavy Component

[0349]

[0350] Table I-4: Characteristics of Hydrocracking Gasoline Products

[0351]

[0352] Table I-5: Characteristics of Mineral-Rich Precursor Substances

[0353]

[0354] Table I-6: Characteristics of Aromatic-Rich Fractions

[0355]

[0356] Example II-1

[0357] Feedstock: The DOA of Example 1-B was mixed with LCO in a weight ratio of 1:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table II-1.

[0358] 1st reaction unit: A mixed feedstock was tested in a medium-sized moving-bed to fixed-bed heavy oil hydroprocessor. Mineral-rich precursor material 1 was loaded into the moving-bed reactor; depending on the flow direction of the reactants, mineral-rich precursor material 2, RDM-33B residue demetallation and desulfurization transfer catalyst, and RCS-31 desulfurization catalyst were loaded into the fixed-bed reactor in the following loading volume ratios: mineral-rich precursor material 1 : mineral-rich precursor material 2 : RDM-33B : RCS-31 = 30 : 36 : 14 : 20. Hydroprocessing was performed at: pressure 16 MPa, volumetric space velocity 0.18 h -1 It was operated under conditions of a hydrogen / oil ratio (by volume) of 1000:1, where hydrogenation in the moving bed reactor was carried out at a temperature of 385°C and hydrogenation in the fixed bed reactor was carried out at a temperature of 370°C. After fixed-bed hydrogenation treatment of the mixed feedstock, the characteristics of the product are presented in Table II-2.

[0359] separation: The liquid product obtained from the hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 335°C or higher were presented in Table II-3.

[0360] 2nd Reaction Unit: Hydrocracking tests were performed on the first light component in a fixed-bed hydrocracking apparatus at a temperature below 335°C with the following catalyst loading ratios: RS-2100: RHC-131 = 40:60 (V / V). The hydrocracking method was: purification section temperature 370°C, cracking section temperature 385°C, reaction pressure 7 MPa, volumetric space velocity 2.0 h -1 and operated under conditions of a hydrogen / oil volume ratio of 1200:1. The characteristics of the obtained hydrocracking gasoline products are presented in Table II-4.

[0361] Example II-2

[0362] Feedstock: The DOA of Example 1-B was mixed with HCO in a weight ratio of 5:10, and the mixed feedstock was liquid at room temperature, and the characteristics of the mixed feedstock are presented in Table II-1.

[0363] 1st reaction unit: The mixed feedstock was tested in a medium-sized moving-bed-fixed-bed heavy oil hydrotreatment apparatus. The catalyst loading and processing conditions were the same as those in the fixed-bed heavy oil hydrotreatment of Example II-1, and the characteristics of the product after hydrotreatment are presented in Table II-2.

[0364] separation: The liquid product obtained from the hydrogenation treatment was fractionated, and the characteristics of the first heavy component at a temperature of 378°C or higher were presented in Table II-3.

[0365] 2nd Reaction Unit: Tests were performed on the first light component at a temperature of less than 378°C in a fixed-bed hydrocracking apparatus. The catalyst and test conditions were the same as those in the hydrocracking test of the first light component at a temperature of less than 378°C in Example II-1, and the hydrocracking products were obtained and their characteristics are presented in Table II-4.

[0366] Table II-1: Characteristics of Mixed Feedstocks

[0367]

[0368] Table II-2: Characteristics of products after heavy oil hydrogenation

[0369]

[0370] Table II-3: Characteristics of the First Heavy Component

[0371]

[0372] Table II-4: Characteristics of Hydrocracking Gasoline Products

[0373]

[0374] Example III-A

[0375] Solvent deasphalting was performed using vacuum residue from the Middle East as a feedstock, and the solvent was a hydrocarbon mixture containing mainly butane (butane content 75 wt%) and small amounts of propane and pentane, wherein solvent deasphalting was performed at 120°C with a solvent:vacuum residue ratio of 4:1 (weight ratio) to obtain a yield of 72.4 wt% deasphalted oil (DAO) and 27.2 wt% de-oiled asphalt (DOA).

[0376] Example III-1

[0377] The DAO and DOA used in this example were both derived from Example III-A, and the characteristics of the DAO and DOA are presented in Table III-1.

[0378] The characteristics of the liquid product obtained from the DAO after passing through the third hydrogenation unit are presented in Table III-1.

[0379] The DCC unit was operated under conditions of a reaction temperature of 410°C, a catalyst-to-oil ratio of 3, and a residence time of 5 seconds; LCO1 (see Table III-6 for characteristics), HCO1, and slurry oil 1 were produced in the DCC unit.

[0380] Slurry oil 1 obtained from the DCC unit passed through the 4th hydrogenation unit (fixed-bed residue oil hydrogenation unit) to provide demetallated slurry oil 1, and its characteristics are presented in Table III-1.

[0381] DOA and demetalized slurry oil 1 were mixed in a weight ratio of 1:10, and the mixed feedstock (see Table III-2 for characteristics) was hydrogenated in the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are presented in Table III-3.

[0382] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0383] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0384] Example III-2

[0385] The DAO and DOA used in this embodiment were the same as those in Example III-1.

[0386] The characteristics of the liquid product obtained from the DAO after passing through the third hydrogenation unit are presented in Table III-1.

[0387] The DCC unit was operated under conditions of a reaction temperature of 420°C, a catalyst-to-oil ratio of 3, and a residence time of 5 seconds; LCO2, HCO2, and slurry oil 2 were produced in the DCC unit.

[0388] Slurry oil 2 obtained from the DCC unit passed through the 4th hydrogenation unit (fixed-bed residue oil hydrogenation unit) to provide demetallated slurry oil 2, and its characteristics are presented in Table III-1.

[0389] DOA and demetalized slurry oil 2 were mixed in a weight ratio of 5:10, and the mixed feedstock (see Table III-2 for characteristics) was hydrogenated in the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are presented in Table III-3.

[0390] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0391] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0392] Example III-3

[0393] The DAO and DOA used in this embodiment were the same as those in Example III-1.

[0394] The characteristics of the liquid product obtained from the DAO after passing through the third hydrogenation unit are presented in Table III-1.

[0395] The DCC unit was operated under conditions of a reaction temperature of 440°C, a catalyst-to-oil ratio of 3, and a residence time of 5 seconds; LCO3, HCO3, and slurry oil 3 were produced in the DCC unit.

[0396] Slurry oil 3 obtained from the DCC unit passed through the 4th hydrogenation unit (fixed-bed residue oil hydrogenation unit) to provide demetallated slurry oil 3, and its characteristics are presented in Table III-1.

[0397] DOA and demetalized slurry oil 3 were mixed in a weight ratio of 10:10, and the mixed feedstock (see Table III-2 for characteristics) was hydrogenated in the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are presented in Table III-3.

[0398] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0399] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0400] Example III-4

[0401] DOA (derived from Example III-A) and demetalized slurry oil 1 were mixed in a weight ratio of 15:10, and the mixed feedstock (characteristics are shown in Table III-2) was hydrogenated in the first hydrogenation unit (fixed-bed residue oil hydrogenation unit). The characteristics of the product are shown in Table III-3.

[0402] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0403] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0404] Example III-5

[0405] DOA (derived from Example III-A) was mixed with LCO1, HCO1, and demetallized slurry oil 1 in a weight ratio of 1:3:3:4, and the mixed feedstock (characteristics are shown in Table III-2) was hydrogenated in the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are shown in Table III-3.

[0406] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0407] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0408] Example III-6

[0409] The first heavy component obtained in Example III-1 was supplied to a delayed coking unit for reaction to obtain coker gasoline.

[0410] The delayed coking unit was operated under conditions of a reaction temperature of 490°C and a residence time of 1.5 hours.

[0411] As a result, coker gasoline was obtained with a yield of 29.7 wt%, and the sulfur weight fraction in the petroleum coke was 2.7%.

[0412] Example III-7

[0413] The procedure of this embodiment was similar to Example III-1, except that the obtained first heavy component was fed to a delayed coking unit for reaction to obtain coker gasoline, coker diesel, and coker wax oil.

[0414] The delayed coking unit was operated under conditions of a reaction temperature of 500°C and a residence time of 1.2 hours.

[0415] As a result, coker gasoline was obtained with a yield of 30.8 wt%, and the sulfur weight fraction in the petroleum coke was 2.5%.

[0416] Coker diesel and coker wax oil were recirculated to the first hydrogenation unit (fixed-bed residue hydrogenation unit) for hydrogenation treatment, where the mixed feedstock (see Table III-2 for its characteristics) consisted of DOA: demetalization slurry 1: coker diesel: coker wax oil in a weight ratio of 1: 5: 3: 2. After hydrogenation treatment, the characteristics of the product are presented in Table III-3.

[0417] The first hydrogenation unit of the example was operated under the same conditions as in Example III-1.

[0418] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0419] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0420] Example III-8

[0421] Tests were performed on the first light component obtained in Example III-1 at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. A diesel component was obtained.

[0422] The catalysts used were the RS-2100 hydrogenation purification catalyst and the RHC-131 hydrocracking catalyst produced by SINOPEC CATALYST CO.,LTD. CHANGLING DIVISION. The loading ratio between the catalysts is as follows: RS-2100 : RHC-131 = 40 : 60 (V / V). The hydrocracking method was as follows: purification section temperature 370°C, cracking section temperature 385°C, reaction pressure 7 MPa, and liquid volume space velocity 2.0 h⁻¹. -1 and operated under conditions of a hydrogen / oil volume ratio of 1200:1. The characteristics of the obtained hydrocracking gasoline products are presented in Table III-4.

[0423] Example III-9

[0424] The same mixed feedstock as in Example III-1 was hydrogenated in the first hydrogenation unit (moving bed residue hydrogenation treatment unit) to obtain a product having the characteristics shown in Table III-3.

[0425] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0426] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0427] Example III-10

[0428] The DOA used in the example (derived from Example III-A) was mixed with refined light oil QY1 and demetalized slurry oil 1 in a weight ratio of 1:5:5, and the mixed feedstock (characteristics are seen in Table III-2) was hydrogenated by the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are presented in Table III-3.

[0429] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0430] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0431] Example III-11

[0432] The DOA used in the example (derived from Example III-A) was mixed with refined light oil QY2 and demetalized slurry oil 1 in a weight ratio of 2:5:5, and the mixed feedstock (characteristics are seen in Table III-2) was hydrogenated by the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are presented in Table III-3.

[0433] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0434] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking unit. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0435] Example III-12

[0436] The DOA used in the example (derived from Example III-A) was mixed with filtered slurry oil 1 (solid content 5 μg / g) in a weight ratio of 1:10, and the mixed feedstock (characteristics are shown in Table III-2) was hydrogenated by the first hydrogenation unit (fixed-bed residue hydrogenation unit). The characteristics of the product are presented in Table III-3.

[0437] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table III-4.

[0438] The characteristics of the obtained hydrogenation cracking products are presented in Table III-5.

[0439] Example III-13

[0440] In this embodiment, the first hard component was recirculated to the DCC unit at a recirculation rate of 0.1 at a temperature of less than 350°C, except that the embodiment was carried out in a manner similar to Example III-1.

[0441] LCO13, HCO13, and slurry oil 13 were produced in the DCC unit.

[0442] Slurry oil 13 obtained from the DCC unit passed through the 4th hydrogenation unit (fixed-bed residue oil hydrogenation unit) to provide demetallated slurry oil 13, and its characteristics are presented in Table III-1.

[0443] DOA and demetalized slurry oil 13 were mixed in a weight ratio of 1:10, and the mixed feedstock (characteristics are shown in Table III-2) was hydrogenated in the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are shown in Table III-3.

[0444] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table III-5.

[0445] Comparative Example III-1

[0446] The catalyst and apparatus were the same as in Example III-1.

[0447] DOA was mixed with light oil QY3 and demetalized slurry oil 1 in a weight ratio of 3:5:5, and DOA did not reach complete dissolution at 100°C.

[0448] The mixed feedstock contained a large amount of solids, so the following experiment could not be performed.

[0449] Table III-1: Characteristics of DOA, DAO, and liquid products after treatment by the third hydrogenation unit

[0450]

[0451] Table III-2: Characteristics of Mixed Feedstocks

[0452]

[0453] Table III-2 (Continued from Table III-2): Characteristics of Mixed Feedstocks

[0454]

[0455] Table III-3: Characteristics of the product after hydrogenation of residue by fixed bed / moving bed in the first hydrogenation unit

[0456]

[0457] Table III-4: Characteristics of the First Heavy Oil Component

[0458]

[0459] Table III-5: Characteristics of Hydrocracking Products

[0460]

[0461] Table III-6

[0462]

[0463] From the data in Table III-4, it can be seen that the technology of the present invention can produce high-quality low-sulfur marine fuel or low-sulfur coke product feedstocks from DOA.

[0464] From the data in Table III-5, it can be seen that the technology of the present invention can produce gasoline products that meet the Country V standards for high quality and low olefin content from DOA.

[0465] Example IV-1

[0466] The DAO and DOA used in this example were both derived from Example IV-A, and the characteristics of the DAO and DOA are presented in Table IV-1.

[0467] The characteristics of the liquid product obtained from the DAO after passing through the third hydrogenation unit are presented in Table IV-1.

[0468] The DCC unit was operated under conditions of a reaction temperature of 410°C, a catalyst-to-oil ratio of 3.0, and a residence time of 3 seconds; LCO1 (see Table IV-6 for characteristics), HCO1 (see Table IV-6 for characteristics), and slurry oil 1 were produced in the DCC unit.

[0469] DOA and LCO1 were mixed in a weight ratio of 1:10, and the mixed feedstock (characteristics are shown in Table IV-2) was hydrogenated in the second hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are shown in Table IV-3.

[0470] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table IV-4.

[0471] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table IV-5.

[0472] Example IV-2

[0473] The DAO and DOA used in this embodiment were the same as those in Example IV-1.

[0474] The characteristics of the liquid product obtained from the DAO after passing through the third hydrogenation unit were the same as in Example IV-1.

[0475] The DCC unit was operated under conditions of a reaction temperature of 420°C, a catalyst-to-oil ratio of 3.0, and a residence time of 3 seconds; LCO2 (see Table IV-6 for characteristics), HCO2, and slurry oil 2 were produced in the DCC unit.

[0476] DOA and LCO2 were mixed in a weight ratio of 5:10, and the mixed feedstock (characteristics are shown in Table IV-2) was hydrogenated in the first hydrogenation unit (fixed-bed residue hydrotreatment unit). The characteristics of the product are shown in Table IV-3.

[0477] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table IV-4.

[0478] Tests were performed on the first light component at a temperature of less than 350°C in a fixed-bed hydrocracking apparatus. The characteristics of the obtained hydrocracking products are presented in Table IV-5.

[0479] Table IV-1: Characteristics of DOA, DAO, and liquid products after treatment by the third hydrogenation unit

[0480]

[0481] Table IV-2: Characteristics of Mixed Feedstocks

[0482]

[0483] Table IV-3: Characteristics of products after fixed-bed / moving-bed hydrogenation of residue in the first hydrogenation unit

[0484]

[0485] Table IV-4: Characteristics of the First Heavy Oil Component

[0486]

[0487] Table IV-5: Characteristics of Hydrocracking Products

[0488]

[0489] Example V-1

[0490] 5th Reaction Unit: The feedstock for the aromatic-rich fractionated oil was LCO1 derived from the catalytic cracking unit of SINOPEC YANGZI PETROCHEMICAL CO., LTD (see Table V-1 for characteristics). The fifth reaction unit was: reaction temperature 290°C, reaction pressure 4 MPa, liquid volume space velocity 1 h -1 and operated under conditions of a hydrogen to oil volume ratio of 800:1.

[0491] First discernment: The second light component and second heavy component 1 (refer to Table V-1 for characteristics) had a cutting point of 180°C;

[0492] 1st reaction unit: Feedstock DOA (derived from vacuum residue of Iranian heavy oil) and Second Heavy Component 1 were mixed in a weight ratio of 1:10, and their characteristics are presented in Table V-2. A medium-sized fixed-bed residue hydrotreatment unit with a total reactor volume of 200 mL was used. Depending on the flow direction of the reactants, RG-30B protective catalyst, mineral-rich precursor material 1, mineral-rich precursor material 2, RDM-33B residue demetallation and desulfurization transfer catalyst, and RCS-31 desulfurization catalyst were sequentially loaded into the first reaction unit in the following loading volume ratios: RG-30B: mineral-rich precursor material V-1: mineral-rich precursor material V-2: RDM-33B: RCS-31 = 6: 30: 30: 14: 20 (V / V). The operating conditions are as follows: reaction temperature 360℃, reaction pressure 8 MPa, liquid volume space velocity 0.3 h -1 and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table V-3.

[0493] Second discernment: The liquid product obtained by treatment of the first reaction unit was fractionated to provide a first light component at a temperature below 350°C and a first heavy component at a temperature above 350°C, and the characteristics of the first heavy component are presented in Table V-4.

[0494] The first hard component was tested in the second reaction unit.

[0495] 2nd Reaction Unit: RS-2100: RHC-131 were sequentially loaded into a fixed-bed hydrocracking device at a ratio of 40:60 (V / V), with a purification section reaction temperature of 370°C, a cracking section reaction temperature of 385°C, a reaction pressure of 10 MPa, and a liquid volume space velocity of 2.0 h⁻¹. -1 and operated under conditions of a hydrogen / oil volume ratio of 1200:1. The characteristics of the obtained hydrocracking products are presented in Table V-5.

[0496] Example V-2

[0497] 5th Reaction Unit: The feedstock for the aromatic-rich fracttown sea oil was HCO2 derived from the catalytic cracking unit of SINOPEC ZHENHAI REFINNING & CHEMICAL COMPANY (see Table V-1 for characteristics). The fifth reaction unit was: reaction temperature 330°C, reaction pressure 6 MPa, liquid volume space velocity 1 h -1 and operated under conditions of a hydrogen to oil volume ratio of 800:1.

[0498] First discernment: The second light component and second heavy component 2 (refer to Table V-1 for characteristics) had a cutting point of 190°C;

[0499] 1st reaction unit: Feedstock DOA (derived from vacuum residue of Iranian heavy oil) and Second Heavy Component 2 were mixed in a weight ratio of 5:10, and their characteristics are presented in Table V-2. The processing apparatus and catalyst loading were identical to those in Example V-1. The operating conditions were as follows: reaction temperature 380°C, reaction pressure 10 MPa, liquid volume space velocity 0.3 h⁻¹ -1 and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table V-3.

[0500] Second discernment: The liquid product obtained by treatment of the first reaction unit was fractionated to provide a first light component at a temperature below 350°C and a first heavy component at a temperature above 350°C, and the characteristics of the first heavy component are presented in Table V-4.

[0501] The first hard component was tested in the second reaction unit.

[0502] 2nd Reaction Unit: In the same manner as in Example V-1, the hydrocracking product was obtained, and its characteristics are presented in Table V-5.

[0503] Example V-3

[0504] 5th Reaction Unit: The feedstock for the aromatic-rich fractionated oil was LCO1 derived from the catalytic cracking unit of SINOPEC YANGZI PETROCHEMICAL CO., LTD (see Table V-1 for characteristics). The fifth reaction unit was: reaction temperature 320°C, reaction pressure 6 MPa, liquid volume space velocity 1 h -1 and operated under conditions of a hydrogen to oil volume ratio of 800:1.

[0505] First discernment: The second light component and second heavy component 3 (refer to Table V-1 for characteristics) had a cutting point of 190°C;

[0506] 1st reaction unit: Feedstock DOA (derived from vacuum residue of Iranian heavy oil) and Second Heavy Component 3 were mixed in a weight ratio of 10:10, and their characteristics are presented in Table V-2. The processing apparatus and catalyst loading were identical to those in Example V-1. The operating conditions were as follows: reaction temperature 370°C, reaction pressure 6 MPa, liquid volume space velocity 0.3 h⁻¹ -1 and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table V-3.

[0507] Second discernment: The liquid product obtained by treatment of the first reaction unit was fractionated to provide a first light component at a temperature below 350°C and a first heavy component at a temperature above 350°C, and the characteristics of the first heavy component are presented in Table V-4.

[0508] The first heavy component was coked at a reaction temperature of 500°C for a residence time of 0.5 hours to obtain petroleum coke with a sulfur content of 2.7 wt% (yield 30 wt%).

[0509] The first hard component was tested in the second reaction unit.

[0510] 2nd Reaction Unit: The process was identical to Example V-1, and the hydrocracking product was obtained and its characteristics are presented in Table V-5.

[0511] Table V-1: Characteristics of aromatic-rich fraction oils before and after hydrogenation

[0512]

[0513] Table V-2: Characteristics of Mixed Feedstocks

[0514]

[0515] Table V-2 (continued): Characteristics of mixed feedstocks

[0516]

[0517] Table V-3: Characteristics of products after hydrogenation of mixed feedstocks

[0518]

[0519] Table V-4: Characteristics of the first heavy component

[0520]

[0521] Table V-5: Characteristics of Hydrocracking Products

[0522]

[0523] Example VI-B

[0524] Solvent deasphalting was performed using vacuum residue as a feedstock, and the solvent was a hydrocarbon mixture containing butane (butane content 75 wt%), wherein solvent deasphalting was performed at 120°C with a solvent:vacuum residue ratio of 2:1 (weight ratio) to obtain a yield of 68 wt% DAO and 32 wt% DOA.

[0525] The characteristics of the obtained DAO and DOA are presented in Table VI-1.

[0526] Example VI-1

[0527] The DAO and DOA used in this example were derived from Example VI-B.

[0528] The characteristics of the liquid product obtained from the DAO that underwent a hydrogenation reaction in the 6th hydrogenation unit are shown in Table VI-1; the liquid product was fed to the DCC unit for reaction to obtain LCO1 (final distillation point 350°C and aromatic content 54%) and HCO1.

[0529] LCO1 was hydrogenated to saturate in the fifth hydrogenation unit and then fractionated to obtain the second light component 1 and the second heavy component 1, with a cutoff point of 180°C. The fifth hydrogenation unit was: reaction temperature 290°C, reaction pressure 4 MPa, liquid volume space velocity 1 h⁻¹ -1 and operated under conditions of a hydrogen to oil volume ratio of 800:1. The characteristics of LCO1 and the second heavy component 1 are presented in Table VI-2.

[0530] DOA and the second heavy component 1 were mixed in a weight ratio of 1:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0531] The first reaction unit was operated for a mixed feedstock of DOA and Second Heavy Component 1 under the following conditions: reaction temperature 360°C, reaction pressure 8 MPa, liquid volume space velocity 0.3 h -1and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table VI-4.

[0532] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0533] Tests were performed on the first light component at a temperature of less than 350°C in the second reaction unit to obtain the hydrocracking product, and its characteristics are presented in Table VI-6.

[0534] Example VI-2

[0535] The DAO and DOA used in this example were derived from Example VI-B.

[0536] The characteristics of the liquid product obtained from the DAO that underwent the hydrogenation reaction in the 6th hydrogenation unit are shown in Table VI-1; the liquid product was fed to the DCC unit for reaction to obtain LCO2 and HCO2.

[0537] HCO2 was hydrogenated to saturate in the fifth hydrogenation unit and then fractionated to obtain the second light component 2 and the second heavy component 2, with a cutoff point of 180°C. The fifth hydrogenation unit was: reaction temperature 330°C, reaction pressure 6 MPa, liquid volume space velocity 1 h -1 and operated under conditions of a hydrogen to oil volume ratio of 800:1. The characteristics of HCO2 and the second heavy component 2 are presented in Table VI-2.

[0538] DOA and the second heavy component 2 were mixed in a weight ratio of 5:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0539] The first reaction unit was operated for a mixed feedstock of DOA and second heavy component 2 under the following conditions: reaction temperature 380°C, reaction pressure 10 MPa, liquid volume space velocity 0.3 h -1and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table VI-4.

[0540] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0541] Tests were performed on the first light component at a temperature of less than 350°C in the second reaction unit to obtain the hydrocracking product, and its characteristics are presented in Table VI-6.

[0542] Example VI-3

[0543] The DAO and DOA used in this example were derived from Example VI-B.

[0544] The characteristics of the liquid product obtained from the DAO that underwent the hydrogenation reaction in the 6th hydrogenation unit are shown in Table VI-1; the liquid product was fed to the DCC unit for reaction to obtain LCO1 and HCO1.

[0545] LCO1 was hydrogenated to saturate in the fifth hydrogenation unit and then fractionated to obtain the second light component 3 and the second heavy component 3, with a cutoff point of 180°C. The fifth hydrogenation unit had: a reaction temperature of 320°C, a reaction pressure of 6 MPa, and a liquid volume space velocity of 1 h⁻¹. -1 and operated under conditions of a hydrogen to oil volume ratio of 800:1. The characteristics of LCO1 and the second heavy component 3 are presented in Table VI-2.

[0546] DOA and the second heavy component 3 were mixed in a weight ratio of 10:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0547] The first reaction unit was operated for a mixed feedstock of DOA and the second heavy component 3 under the following conditions: reaction temperature 370°C, reaction pressure 6 MPa, liquid volume space velocity 0.3 h -1and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table VI-4.

[0548] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0549] The first heavy component was coked at a reaction temperature of 500°C for a residence time of 0.5 hours to obtain petroleum coke with a sulfur content of 2.6 wt% (yield 31 wt%).

[0550] Tests were performed on the first light component at a temperature of less than 350°C in the second reaction unit to obtain the hydrocracking product, and its characteristics are presented in Table VI-6.

[0551] Example VI-4

[0552] The DAO and DOA used in this example were derived from Example VI-B.

[0553] The characteristics of the liquid product obtained from the DAO that underwent the hydrogenation reaction in the 6th hydrogenation unit are shown in Table VI-1; the liquid product was fed to the DCC unit for reaction to obtain LCO1 and HCO1.

[0554] The aromatic-rich fraction oil used in this example was coal tar from a coal tar unit in China (see Table VI-1 for characteristics) and LCO1. LCO1 and coal tar were used in a weight ratio of 1:1. The aromatic-rich fraction oil was hydrogenated and saturated in the fifth hydrogenation unit and then fractionated to obtain the second light component 4 and the second heavy component 4, with a cutoff point of 180°C. The fifth hydrogenation unit had: a reaction temperature of 300°C, a reaction pressure of 10 MPa, and a liquid volume space velocity of 0.8 h⁻¹ per hour. -1 and operated under conditions of a hydrogen-to-oil volume ratio of 800:1. The characteristics of the aromatic-rich fraction oil and the second heavy component 4 are presented in Table VI-2.

[0555] DOA and the second heavy component 4 were mixed in a weight ratio of 15:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0556] The first reaction unit was operated for a mixed feedstock of DOA and second heavy component 4 under the following conditions: reaction temperature 350°C, reaction pressure 12 MPa, liquid volume space velocity 0.3 h -1 and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table VI-4.

[0557] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0558] Tests were performed on the first light component at a temperature of less than 350°C in the second reaction unit to obtain the hydrocracking product, and its characteristics are presented in Table VI-6.

[0559] Example VI-5

[0560] A method similar to Example I-3 was used, except for the following:

[0561] In this embodiment, the hydrogenation treatment temperature of the first reaction unit was 395℃.

[0562] Other conditions were the same as in Example VI-3.

[0563] The characteristics of the mixed feedstock after hydrogenation are presented in Table VI-4.

[0564] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0565] Example VI-6

[0566] The conditions for catalyst loading and hydrogenation treatment were the same as in Example VI-3.

[0567] After hydrogenating the same mixed feedstock as in Example VI-3 in the first reaction unit, the reaction temperature of the fixed bed was increased by 3°C every 30 days, and the operation was stopped after 360 days of operation of the hydrogenation test.

[0568] Mineral-rich precursor material 1 and mineral-rich precursor material 2, which were initially loaded into the reactor, became V-rich material 1 and V-rich material 2, with V content of 56 wt% and 47 wt%, respectively, by roasting analysis after reaction. These are high-quality materials capable of producing high-value V2O5, with V content more than 10 times higher than that of natural ore.

[0569] Example VI-7

[0570] A catalytic cracking test was conducted on the second light component at a temperature of less than 350°C derived from Example VI-3 using a small-scale catalytic cracking fixed fluidized bed test apparatus, wherein the catalyst was catalytic cracking catalyst MLC-500 produced by SINOPEC CATALYST CO.LTD CHANGLING DIVISION; and the test was operated under conditions of a reaction temperature of 540°C, a catalyst-to-oil ratio of 5, and a residence time of 2 seconds.

[0571] As a result, the product gasoline was obtained in a yield of 43 weight%, and the RON octane rating of the gasoline was 92.

[0572] Example VI-8

[0573] The procedure of this embodiment was similar to Example VI-1, except that the obtained first heavy component was fed to a delayed coking unit for reaction to obtain coker gasoline, coker diesel, and coker wax oil.

[0574] The coker diesel had a sulfur content of 0.16 wt%, a condensation point of -13°C, and a cetane number of 49.

[0575] The delayed coking unit was operated under conditions of a reaction temperature of 500°C and a residence time of 0.5 hours.

[0576] The coker wax oil had a sulfur content of 0.76 wt% and a condensation point of 32°C.

[0577] Coker gasoline was obtained in a yield of 15%, with a sulfur content of 0.08 wt% and MON 60.

[0578] Coker diesel and coker wax oil were recirculated to the fifth hydrogenation unit and mixed with LCO1 for hydrogenation saturation, and then fractionated to obtain a second light component 8 and a second heavy component 8 having a cutting point of 180°C, and the reaction conditions were the same as those in Example VI-1. The characteristics of the mixed oil of coker diesel, coker wax oil, and LCO1 and the characteristics of the second heavy component 8 are presented in Table VI-2.

[0579] DOA of Example VI-B and the second heavy component 8 were mixed in a weight ratio of 1:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0580] The first reaction unit was operated for a mixed feedstock of DOA and Second Heavy Component 8 under the following conditions: reaction temperature 360°C, reaction pressure 8 MPa, liquid volume space velocity 0.3 h -1 and a hydrogen to oil volume ratio of 800:1. After hydrogenation, the characteristics of the mixed feedstock are presented in Table VI-4.

[0581] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0582] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0583] Example VI-9

[0584] A test was conducted on the first light component obtained in Example VI-1 at a temperature of less than 350°C using a diesel hydrogenation upgrade device, and a diesel component was obtained.

[0585] The hydrogenation upgrade device has: a reaction temperature of 350℃, a reaction pressure of 7 MPa, a hydrogen-to-oil volume ratio of 800, and a liquid volume space velocity of 1.0 h -1 It was operated under the conditions of.

[0586] As a result, the obtained diesel component had a sulfur content of 9 ppm, a condensation point of -32°C, and a cetane number of 51.9.

[0587] Example VI-10

[0588] The procedure of this example was similar to Example VI-1, except that the loading of the catalyst in the first reaction unit was as follows:

[0589] According to the flow direction of the reactants, the hydrogenation protection catalyst, mineral-rich precursor material 1, hydrogenation demetallation and desulfurization catalyst, and hydrogenation desulfurization catalyst were loaded sequentially. The loading ratio between the catalysts in the first reaction unit is as follows: RG-30B: mineral-rich precursor material 1: RDM-33B: RCS-31 = 6: 60: 14: 20 (V / V).

[0590] The characteristics of the mixed feedstock after hydrogenation are presented in Table VI-4.

[0591] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0592] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0593] Example VI-11

[0594] The procedure of this example was similar to Example VI-1, except that the loading of the catalyst in the first reaction unit was as follows:

[0595] Depending on the flow direction of the reactants, the hydrogenation protection catalyst, mineral-rich precursor material 2, mineral-rich precursor material 1, hydrogenation demetallation and desulfurization catalyst, and hydrogenation desulfurization catalyst were loaded sequentially. The loading ratio between the catalysts in the first reaction unit is as follows: RG-30B: mineral-rich precursor material 2: mineral-rich precursor material 1: RDM-33B: RCS-31 = 6: 30: 30: 14: 20 (V / V).

[0596] The characteristics of the mixed feedstock after hydrogenation are presented in Table VI-4.

[0597] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0598] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0599] Example VI-12

[0600] The procedure of this example was similar to Example VI-1, except that the loading of the catalyst in the first reaction unit was as follows:

[0601] According to the flow direction of the reactants, the hydrogenation protection catalyst, the hydrogenation demetallation and desulfurization catalyst, and the hydrogenation desulfurization catalyst were loaded sequentially. In the first reaction unit, the loading ratio between the catalysts is as follows: RG-30B: RDM-33B: RCS-31 = 12: 38: 50 (V / V).

[0602] The characteristics of the mixed feedstock after hydrogenation are presented in Table VI-4.

[0603] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0604] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0605] Example VI-13

[0606] The procedure of this example was similar to Example VI-1, except that the loading of the catalyst in the first reaction unit was as follows:

[0607] According to the flow direction of the reactants, the hydrogenation protection catalyst, mineral-rich precursor material 3, hydrogenation demetallation and desulfurization catalyst, and hydrogenation desulfurization catalyst were loaded sequentially. In the first reaction unit, the loading ratio between the catalysts is as follows: RG-30B: mineral-rich precursor material 3: RDM-33B: RCS-31 = 5: 40: 20: 35 (V / V).

[0608] The characteristics of the mixed feedstock after hydrogenation are presented in Table VI-4.

[0609] The liquid product obtained from the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0610] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0611] Comparative Example VI-1

[0612] The catalyst and apparatus were similar to those in Example VI-1, except for the following:

[0613] In this comparative example, the aromatic-rich fraction oil QY (aromatic content 20 wt%) was mixed directly with DOA without passing through a partial hydrogenation saturation unit. DOA and QY were mixed in a weight ratio of 1:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0614] After hydrogenating the mixed feedstock in the first reaction unit, the characteristics of the product are presented in Table VI-4.

[0615] The liquid product obtained by hydrogenation treatment in the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0616] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0617] Comparative Example VI-2

[0618] The catalyst and apparatus were similar to those in Example VI-1, except for the following:

[0619] In this comparative example, the aromatic-rich fraction oil QY was mixed directly with DOA without passing through a partial hydrogenation saturation unit. DOA and QY were mixed in a weight ratio of 2:10, and the characteristics of the mixed feedstock are presented in Table VI-3.

[0620] After hydrogenating the mixed feedstock in the first reaction unit, the characteristics of the product are presented in Table VI-4.

[0621] The liquid product obtained by hydrogenation treatment in the first hydrogenation unit was fractionated, and the characteristics of the first heavy component at a temperature of 350°C or higher were presented in Table VI-5.

[0622] The first light component at a temperature of less than 350°C was tested in the second reaction unit to obtain a hydrocracking product, and its characteristics are presented in Table VI-6.

[0623] Comparative Example VI-3

[0624] The catalyst and apparatus were similar to those in Example VI-1, except for the following:

[0625] In this comparative example, the aromatic-rich fraction oil QY was mixed directly with DOA without passing through a partial hydrogenation saturation unit. DOA and QY were mixed in a weight ratio of 3:10. The mixed feedstock contained a large amount of solids (at 100°C), so the subsequent experiment could not be performed.

[0626] Table VI-1: Characteristics of DOA, DAO, and liquid products after hydrogenation in the 6th hydrogenation unit

[0627]

[0628] Table VI-2: Characteristics of Aromatic Rich Fraction Oils Before and After Hydrogenation

[0629]

[0630] Table VI-3: Characteristics of Mixed Feedstocks

[0631]

[0632] Table VI-3 (continued): Characteristics of mixed feedstock

[0633]

[0634] Table VI-4: Characteristics of Products After Hydrogenation of Mixed Feedstocks

[0635]

[0636] Table VI-5: Characteristics of the First Heavy Oil Component

[0637]

[0638] Table VI-6: Characteristics of Hydrocracking Products

[0639]

[0640] Table VI-7: Characteristics of Mineral-Rich Precursor Substances

[0641]

[0642] From the above results, it can be seen that the technology of the present invention enables high-quality raw materials for producing low-sulfur marine fuel or low-sulfur coke products from DOA.

[0643] In addition, the technology of the present invention can provide high-quality gasoline products that meet the national V standards.

[0644] Although preferred embodiments of the present invention have been described in detail above, the present invention is not limited thereto. Within the scope of the technical concept of the present invention, many simple modifications may be made to the technical solution of the present invention, including combining various technical features in other appropriate ways, and such simple modifications and combinations should be considered as part of the disclosure of the present invention and are all within the scope of the present invention.

Claims

Claim 1 A method for processing a heavy oil feedstock, comprising: (1) introducing the heavy oil feedstock into a solvent deasphalting unit for solvent deasphalting treatment to provide deasphalted asphalt and deasphalted oil; (2) introducing a mixed feedstock obtained by mixing deasphalted asphalt and an aromatic-containing stream into a first reaction unit for a hydrogenation reaction, wherein the composition and ratio of the deasphalted asphalt and the aromatic-containing stream are such that the mixed feedstock becomes a liquid state at a temperature of 400°C or lower; (11) introducing the deasphalted oil into a third hydrogenation unit for a hydrogenation reaction to obtain a liquid effluent, and introducing the liquid effluent obtained from the third hydrogenation unit into a DCC unit for reaction to provide propylene, LCO, HCO, and slurry oil; (21) separating the liquid product from the first reaction unit into a first light component and a first heavy component, wherein the first light component and the first heavy component have a cutting point A method comprising: a step of 240-450°C, wherein separation is performed by fractional distillation; (31) a step of introducing a first light component into a second reaction unit for reaction to provide at least one product selected from the group consisting of a gasoline component, a diesel component and a BTX feedstock component, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit and a diesel hydrogenation upgrading unit; and (32) a step of introducing a first heavy component into a delayed coking unit for reaction to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil and low-sulfur petroleum coke; or a step of using the first heavy component as a component of low-sulfur marine fuel oil. Claim 2 In claim 1, in step (2), the oil-free asphalt and aromatic-containing stream is a mixed feedstock formed from the oil-free asphalt and aromatic-containing stream, with a viscosity of 400 mm at 100°C. 2 A method used at a rate that makes it less than or equal to / s. Claim 3 Method according to claim 1, wherein in step (2), the aromatic-containing stream is an aromatic-rich fraction oil and / or an aromatic compound. Claim 4 In paragraph 3, (i) the aromatic-rich fraction oil has a distillation endpoint of 200–540°C and an aromatic hydrocarbon content of 20 weight% or more; the aromatic-rich fraction oil is at least one selected from the group consisting of LCO, HCO, ethylene tar, coal tar, coker diesel, and coker wax oil; or (ii) the aromatic compound is benzene, toluene, xylene, naphthalene, at least one C 1-6 At least one selected from the group consisting of alkyl-substituted naphthalene and tricyclic or higher aromatic hydrocarbons; or (iii) the aromatic-rich fraction oil has a distillation endpoint of 200-540°C and an aromatic hydrocarbon content of 20 wt% or more; the aromatic-rich fraction oil is at least one selected from the group consisting of LCO, HCO, ethylene tar, coal tar, coker diesel, and coker wax oil, and the aromatic compound is benzene, toluene, xylene, naphthalene, at least one C 1-6 A method comprising at least one selected from the group consisting of naphthalene substituted with an alkyl group and three or more aromatic hydrocarbons. Claim 5 In paragraph 3, in step (2), the aromatic-containing stream is an aromatic-rich fractional oil, and the deoiled asphalt and the aromatic-containing stream are used in a weight ratio of 1:10 to 50:

10. Claim 6 In paragraph 3, in step (2), the aromatic-containing stream is an aromatic compound, and the degreased asphalt and the aromatic compound are used in a weight ratio of 1:10 to 50:

10. Claim 7 In claim 1, in step (2), the de-oiled asphalt is de-oiled asphalt obtained by solvent de-asphalting a heavy oil feedstock in a solvent de-asphalting unit; the de-oiled asphalt in the solvent de-asphalting unit is obtained in a yield of 50% by weight or less. Claim 8 A method according to any one of claims 1 to 7, further comprising the step of recirculating the coker diesel and / or coker wax oil obtained in step (32) back to step (2) as at least part of an aromatic-containing stream. Claim 9 In any one of claims 1 to 7, in step (2), the first reaction unit is: reaction temperature 280-450°C, reaction pressure 8.0-20.0 MPa, hydrogen-to-oil volume ratio 400-2000, and liquid volume space velocity 0.05-1.2 h -1 A method that operates under the conditions of. Claim 10 In any one of claims 1 to 7, in step (31), the second reaction unit is a hydrocracking unit, wherein (i) the hydrocracking unit has a reaction temperature of 330-420°C, a reaction pressure of 5.0-18.0 MPa, a hydrogen-to-oil volume ratio of 500-2000, and a liquid volume space velocity of 0.3-3.0 h -1 (ii) operated under the conditions of; or (ii) the hydrocracking unit is loaded with at least one hydrotreatment catalyst and at least one hydrocracking catalyst; or (iii) the hydrocracking unit is operated under the conditions of a reaction temperature of 330-420°C, a reaction pressure of 5.0-18.0 MPa, a hydrogen-to-oil volume ratio of 500-2000, and a liquid volume space velocity of 0.3-3.0 h -1 A method operated under the conditions of, wherein at least one hydrogenation treatment catalyst and at least one hydrocracking catalyst are loaded into the hydrocracking unit. Claim 11 A method according to any one of claims 1 to 7, wherein in step (31), the second reaction unit is a catalytic decomposition unit, and the catalytic decomposition unit is a fluidized catalytic decomposition unit; the fluidized catalytic decomposition unit is operated under conditions of: a reaction temperature of 500-600°C, a catalyst-to-oil ratio of 3-12, and a residence time of 1-10 seconds. Claim 12 In any one of claims 1 to 7, in step (31), the second reaction unit is a diesel hydrogenation upgrade unit, wherein (i) the diesel hydrogenation upgrade unit has: a reaction temperature of 330-420°C, a reaction pressure of 5.0-18.0 MPa, a hydrogen-to-oil volume ratio of 500-2000, and a liquid volume space velocity of 0.3-3.0 h -1 (ii) operated under the conditions of; or (ii) at least one diesel hydrogenation upgrade catalyst is loaded into the diesel hydrogenation upgrade unit; or (iii) the diesel hydrogenation upgrade unit is: reaction temperature 330-420°C, reaction pressure 5.0-18.0 MPa, hydrogen-to-oil volume ratio 500-2000 and liquid volume space velocity 0.3-3.0 h -1 A method that operates under the conditions of, wherein at least one diesel hydrogenation upgrade catalyst is loaded into the diesel hydrogenation upgrade unit. Claim 13 In any one of claims 1 to 7, (i) in step (32), the first heavy component is introduced into a delayed coking unit for reaction to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke, and the delayed coking unit is operated under conditions of: a reaction temperature of 440-520°C and a residence time of 0.1-4 hours; or (ii) in step (32), the first heavy component has a sulfur content of 1.8 weight% or less, and the first heavy component is introduced into a delayed coking unit for reaction to provide low-sulfur petroleum coke, and the low-sulfur petroleum coke has a sulfur content of 3 weight% or less; or (iii) in step (32), the first heavy component has a sulfur content of 1.8 wt% or less, the first heavy component is introduced into a delay coking unit for reaction to provide low-sulfur petroleum coke, the low-sulfur petroleum coke has a sulfur content of 3 wt% or less, and the delay coking unit is operated under conditions of: a reaction temperature of 440-520°C and a residence time of 0.1-4 hours. Claim 14 A method according to any one of claims 1 to 7, wherein in step (32), the first heavy component is useful as a low-sulfur marine fuel oil component, and the low-sulfur marine fuel oil component has a sulfur content of 0.5 weight% or less. Claim 15 A method according to claim 1, wherein the first reaction unit is a fixed-bed hydrogenation unit, a moving-bed-fixed-bed hydrogenation combined unit, or a moving-bed hydrogenation unit; wherein the third hydrogenation unit is a fixed-bed hydrogenation unit. Claim 16 The method according to claim 1, wherein the first reaction unit comprises a mineral-rich precursor material and / or a hydrogenation catalyst, the hydrogenation catalyst can catalyze at least one reaction selected from a hydrodemetallization reaction, a hydrodesulfurization reaction, a hydrodeasphalting reaction and a hydrodecarbonization reaction, and the mineral-rich precursor material is a material capable of adsorbing at least one metal selected from V, Ni, Fe, Ca and Mg. Claim 17 In claim 16, (i) in step (2), the mineral-rich precursor material comprises a support and an active component element loaded on the support, wherein the support is at least one selected from the group consisting of aluminum hydroxide, alumina, and silica, and the active component element is at least one metal element selected from Group VIB and Group VIII; or (ii) in step (2), the mineral-rich precursor material has a loss on ignition of 3 weight% or more, 80 m 2 or (iii) having a specific surface area of ​​0.9 g / g or more and a water absorption rate of 0.9 g / g or more; or (iii) in step (2), the mineral-rich precursor material comprises a support and an active component element loaded on the support, the support is at least one selected from the group consisting of aluminum hydroxide, alumina, and silica, and the active component element is at least one metal element selected from groups VIB and VIII, and the mineral-rich precursor material has a loss on ignition of 3 weight% or more, 80 m 2 A method having a specific surface area of ​​0.9 g / g or more and a water absorption rate of 0.9 g / g or more. Claim 18 In claim 16, in step (2), a mineral-rich first precursor material and a mineral-rich second precursor material are sequentially loaded into a first reaction unit according to the flow direction of the reactants, and the mineral-rich second precursor material has a loss of ignition equal to or greater than that of the mineral-rich first precursor material. Claim 19 A method according to claim 18, wherein in step (2), (i) the mineral-rich first precursor material has a loss on ignition of 3-15 weight% and the mineral-rich second precursor material has a loss on ignition of 15 weight% or more; (ii) the mineral-rich first precursor material and the mineral-rich second precursor material are loaded in a volume ratio of 5:95 to 95:5; or (iii) the mineral-rich first precursor material has a loss on ignition of 3-15 weight% and the mineral-rich second precursor material has a loss on ignition of 15 weight% or more, and the mineral-rich first precursor material and the mineral-rich second precursor material are loaded in a volume ratio of 5:95 to 95:

5. Claim 20 A method according to claim 1, wherein in step (2), the first reaction unit is a moving bed-fixed bed hydrogenation coupling unit, and a mineral-rich precursor material is loaded in the moving bed, and a mineral-rich precursor material and a hydrogenation catalyst are sequentially loaded in the fixed bed, or a hydrogenation catalyst is loaded in the fixed bed. Claim 21 A method according to claim 20, wherein the ratio of the volume of the mineral-rich precursor material loaded on the moving bed to the volume of the mineral-rich precursor material and the hydrogenation catalyst loaded on the fixed bed is 10:90 to 60:

40. Claim 22 The method of claim 20 further comprises the step of replacing a mineral-rich precursor material loaded on a moving bed with a new mineral-rich precursor material at each period, wherein the replacement rate is 5-20 weight% with respect to the total amount of mineral-rich precursor material loaded on the moving bed; and the period is 5-20 days. Claim 23 The method of claim 1, wherein the aromatic-containing stream further comprises an aromatic-rich fraction oil, and the aromatic-rich fraction oil comprises LCO and / or HCO obtained from a DCC unit. Claim 24 A method according to claim 1, wherein in step (11), the operating conditions of the DCC unit are adjusted so that the aromatic content of LCO and / or HCO is 60 weight% or more. Claim 25 In claim 1, at step (11), the third hydrogenation unit has: a reaction temperature of 280-400°C, a reaction pressure of 6.0-14.0 MPa, a hydrogen-to-oil volume ratio of 600-1200, and a liquid space velocity of 0.3-2.0 h per hour. -1 A method that operates under the conditions of. Claim 26 A method according to claim 1, wherein in step (11), at least two hydrogenation catalysts are loaded into the third hydrogenation unit; (i) wherein the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction; (ii) wherein the hydrogenation catalyst comprises alumina as a support and a metal element of group VIB and / or group VIII as an active component element, and optionally at least one auxiliary element selected from P, Si, F and B; or (iii) wherein the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction, and comprises alumina as a support and a metal element of group VIB and / or group VIII as an active component element, and optionally at least one auxiliary element selected from P, Si, F and B. Claim 27 In claim 1, in step (2), the first reaction unit is a fixed-bed hydrogenation unit, and at least two hydrogenation catalysts are loaded into the first reaction unit; (i) where the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of an asphaltene conversion reaction, a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction; or (ii) where the hydrogenation catalyst comprises alumina as a support and a metal element of group VIB and / or group VIII as an active component element, and optionally also comprises at least one auxiliary element selected from P, Si, F and B; or (iii) where the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of asphaltene conversion reaction, hydrogenation demetallation reaction, hydrogenation desulfurization reaction and hydrogenation decarbonization reaction, and comprises alumina as a support and a metal element of group VIB and / or group VIII as an active component element, and optionally also comprises at least one auxiliary element selected from P, Si, F and B. Claim 28 In claim 1, in step (2), the first reaction unit is a moving bed hydrogenation unit, and at least one moving bed hydrogenation catalyst is loaded into the first reaction unit; wherein the moving bed hydrogenation catalyst comprises alumina as a support and a metal element of group VIB and / or group VIII as an active component element, and optionally further comprises at least one auxiliary element selected from P, Si, F and B. Claim 29 The method of claim 1, further comprising: (13) introducing slurry oil obtained from a DCC unit into a fourth hydrogenation unit for a demetalization reaction to provide demetalization slurry oil; and an aromatic-containing stream comprising slurry oil obtained from a DCC unit and / or demetalization slurry oil obtained from a fourth hydrogenation unit into the aromatic-containing stream in step (2) or being used as an aromatic-containing stream in step (2). Claim 30 A method according to claim 29, further comprising the step of recirculating the coker diesel and / or coker wax oil obtained in step (32) back to step (2) as at least part of an aromatic-containing stream. Claim 31 In claim 29, at step (13), the fourth hydrogenation unit is a fixed-bed hydrogenation unit, and the fourth hydrogenation unit has: a reaction temperature of 200-280°C, a reaction pressure of 3.0-6.0 MPa, a hydrogen-to-oil volume ratio of 600-1200 and a liquid space velocity of 0.5-2.5 h -1 A method that operates under the conditions of. Claim 32 A method according to claim 1, further comprising the step of incorporating LCO and / or HCO obtained from a DCC unit into an aromatic-containing stream in step (2). Claim 33 A method according to claim 32, further comprising the step of recirculating the slurry oil obtained from the DCC unit back to the solvent deasphalting unit for solvent deasphalting. Claim 34 A method according to any one of claims 1 to 7, further comprising: step (16): introducing an aromatic-rich fraction into a fifth reaction unit for hydrosaturation and fractionating to provide a second light component and a second heavy component, wherein the second light component and the second heavy component have a cutting point of 100-250°C and the aromatic content in the second heavy component is 20% by weight or more; and the step of incorporating the second heavy component into the aromatic-containing stream in step (2). Claim 35 In claim 34, at step (2), the aromatic-containing stream further comprises an aromatic hydrocarbon and / or an aromatic oil, wherein the aromatic oil is at least one selected from the group consisting of LCO, HCO, FGO, ethylene tar, coal tar, coker diesel and coker wax oil. Claim 36 A method according to claim 34, wherein the aromatic hydrocarbon content in the aromatic-rich fraction oil is 20 weight% or more. Claim 37 In paragraph 34, at step (16), the fifth reaction unit is at least one of a fixed-bed reactor, a moving-bed reactor, and a boiling-bed reactor; wherein the fifth reaction unit has: a reaction temperature of 200-420°C, a reaction pressure of 2-18 MPa, and a liquid space velocity of 0.3-10 h per hour. -1 and a method operated under conditions of a hydrogen-to-oil volume ratio of 50-5000. Claim 38 A method according to claim 34, further comprising: (1) introducing a heavy oil feedstock into a solvent deasphalting unit for solvent deasphalting treatment to provide deasphalted asphalt and deasphalted oil; (14) introducing the deasphalted oil into a sixth hydrogenation unit for a hydrogenation reaction, and introducing the liquid effluent obtained from the sixth hydrogenation unit into a DCC unit for reaction to provide propylene, LCO, HCO and slurry oil, wherein the sixth hydrogenation unit is a fixed-bed hydrogenation unit; and further comprising the step of LCO and / or HCO from the DCC unit being incorporated into an aromatic-rich fraction oil in step (16) or being used as an aromatic-rich fraction oil in step (16). Claim 39 In claim 38, the DCC unit is operated under conditions of: a reaction temperature of 500-650°C, a catalyst-to-oil ratio of 3-12, and a residence time of 0.6-6 seconds, in a method. Claim 40 A method according to claim 38, further comprising the step of recirculating the coker diesel and / or coker wax oil obtained in step (32) back to the fifth reaction unit for hydrosaturation. Claim 41 In paragraph 38, at step (14), the 6th hydrogenation unit is: reaction temperature 280-400°C, reaction pressure 6.0-14.0 MPa, hydrogen-to-oil volume ratio 600-1200 and liquid volume space velocity 0.3-2.0 h -1 A method operated under the conditions of; at step (14), at least two hydrogenation catalysts are loaded into the sixth hydrogenation unit; (i) the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction; (ii) the hydrogenation catalyst comprises alumina as a support and a group VIB and / or group VIII metal element as an active component element, and optionally further comprises at least one auxiliary element selected from P, Si, F and B; or (iii) the hydrogenation catalyst is a catalyst capable of catalyzing at least one reaction selected from the group consisting of a hydrogenation demetallation reaction, a hydrogenation desulfurization reaction, and a hydrogenation decarbonization reaction, comprising alumina as a support and a group VIB and / or group VIII metal element as an active component element, and optionally further comprises at least one auxiliary element selected from P, Si, F and B. Claim 42 As a processing system for heavy oil feedstock, a solvent deasphalting unit used for solvent deasphalting treatment of a heavy oil feedstock to provide deasphalted asphalt and deasphalted oil; a third hydrogenation unit fluidly communicating with the solvent deasphalting unit, wherein the third hydrogenation unit is a fixed-bed hydrogenation unit for hydrogenating the deasphalted oil from the solvent deasphalting unit; and a DCC unit fluidly communicating with the third hydrogenation unit for reacting a liquid effluent obtained from the third hydrogenation unit to provide propylene, LCO, HCO, and slurry oil. A first reaction unit which is a fixed-bed hydrogenation unit or a moving-bed hydrogenation unit, wherein the first reaction unit is in fluid communication with the DCC unit and the solvent deasphalting unit for the conversion reaction of de-oiled asphalt from the solvent deasphalting unit and LCO and / or HCO from the DCC unit; a separation unit that is in fluid communication with the first reaction unit and the DCC unit, respectively, for the first light component obtained from the separation unit to be recirculated back to the DCC unit and for fractionating the liquid effluent from the first reaction unit to obtain the first light component and the first heavy component; a second reaction unit that is in fluid communication with the separation unit for the reaction of the first light component obtained from the separation unit to provide at least one product selected from the group consisting of a gasoline fraction, a diesel fraction, and a BTX feedstock component; and the first heavy component obtained from the separation unit to provide at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke. A system comprising a delay coking unit that communicates fluidly with a separation unit for a reaction. Claim 43 In paragraph 42, the delay coking unit is a system that fluidly communicates with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delay coking unit back to the first reaction unit. Claim 44 In claim 42, the system further comprises a fourth hydrogenation unit fluidly communicating with a DCC unit for demetallating the slurry oil obtained from a DCC unit to provide a demetallated slurry oil; wherein the first reaction unit fluidly communicates with the DCC unit, the fourth hydrogenation unit, and the solvent deasphalting unit for a conversion reaction of degass from a solvent deasphalting unit and demetallated slurry oil from the fourth hydrogenation unit and / or slurry oil from the DCC unit; wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit. Claim 45 In paragraph 44, the DCC unit is in fluid communication with the solvent deasphalting unit to recirculate the slurry oil obtained from the DCC unit back to the solvent deasphalting unit for solvent deasphalting. Claim 46 A processing system for an aromatic-rich fractionated oil, comprising: a fifth reaction unit for hydrosaturation and fractionation of the aromatic-rich fractionated oil to provide a second light component and a second heavy component; a first reaction unit, which is a fixed-bed hydrogenation unit fluidly communicating with the fifth reaction unit, for hydrolysis reaction of an aromatic-containing stream containing a second heavy component from the fifth reaction unit and deoiled asphalt; a separation unit fluidly communicating with the first reaction unit for fractionating a liquid product from the first reaction unit to obtain a first light component and a first heavy component; and a second reaction unit fluidly communicating with the separation unit for reaction of the first light component obtained from the separation unit, wherein the second reaction unit is at least one selected from the group consisting of a hydrocracking unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit. A system characterized by comprising a delay coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke. Claim 47 In paragraph 46, the delay coking unit is a system fluidly communicating with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delay coking unit back to the first reaction unit as at least part of an aromatic-containing stream. Claim 48 A system according to claim 46, further comprising a solvent deasphalting unit used to fluidly communicate with a first reaction unit, introduce a heavy oil feedstock, solvent deasphalt the introduced heavy oil feedstock to obtain deasphalted asphalt and deasphalted oil, and introduce the deasphalted asphalt obtained after solvent deasphalting into the first reaction unit. Claim 49 A processing system for heavy oil feedstocks and aromatic-rich fractional oils, comprising: a solvent deasphalting unit used for solvent deasphalting treatment of a heavy oil feedstock in a solvent deasphalting unit to provide deasphalted asphalt and deasphalted oil; a sixth hydrogenation unit fluidly communicating with the solvent deasphalting unit, wherein the sixth hydrogenation unit is a fixed-bed hydrogenation unit for the hydrogenation reaction of deasphalted oil from the solvent deasphalting unit; and a DCC unit fluidly communicating with the sixth hydrogenation unit for the reaction of a liquid effluent obtained from the sixth hydrogenation unit to provide propylene, LCO, HCO, and slurry oil. A fifth reaction unit fluidly communicating with a DCC unit for hydrosaturating and fractionating an aromatic-rich fraction oil containing LCO and / or HCO to provide a second light component and a second heavy component; a first reaction unit, which is a fixed-bed hydrogenation unit fluidly communicating with the fifth reaction unit and a solvent deasphalting unit, for the hydrogenation reaction of an aromatic-containing stream comprising deasphalted pitch from the solvent deasphalting unit and a second heavy component from the fifth reaction unit; a separation unit fluidly communicating with the first reaction unit and the DCC unit, for fractionating a liquid-phase product from the first reaction unit to obtain a first light component and a first heavy component, capable of recirculating the first light component obtained from the separation unit back to the DCC unit; a second reaction unit fluidly communicating with the separation unit for the reaction of the first light component obtained from the separation unit, wherein the second reaction unit is a hydrocracking unit A second reaction unit, at least one selected from the group consisting of a unit, a catalytic cracking unit, and a diesel hydrogenation upgrade unit;A system characterized by comprising a delayed coking unit fluidly communicating with a separation unit for the reaction of a first heavy component obtained from a separation unit, for providing at least one product selected from the group consisting of coker gasoline, coker diesel, coker wax oil, and low-sulfur petroleum coke. Claim 50 In paragraph 49, the delay coking unit is a system that fluidly communicates with the first reaction unit to recirculate the coker diesel and / or coker wax oil obtained from the delay coking unit back to the fifth reaction unit. Claim 51 delete Claim 52 delete

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