Method for producing propylene and low sulfur fuel oil components

Abstract

This method for producing propene and low-sulfur fuel oil components includes the steps of contacting a heavy feedstock with a solvent to extract and separate the heavy feedstock to obtain a deasphalted oil and a deoiled asphalt, contacting the deasphalted oil and optionally a light feedstock with a catalytic conversion catalyst to react with the light feedstock to obtain a reaction product containing propylene, separating a catalytically cracked distillate from the reaction product, and subjecting the catalytically cracked distillate to hydrodesulfurization to obtain a low-sulfur hydrodistillate. The low-sulfur hydrodistillate and / or the deoiled asphalt are suitable as fuel oil components. This method enables the conversion of saturated hydrocarbons in the heavy feedstock to propylene, thereby avoiding the use of saturated hydrocarbons as fuel oil components and achieving favorable economic and social benefits.

Description

Detailed Description of the Invention

[0001] [Technical field] (CROSS-REFERENCE TO RELATED APPLICATIONS) This application claims priority to patent application No. 201911014995.6, filed on October 24, 2019, entitled “Method for Producing More Propylene and Low Sulfur Fuel Oil Components,” which is incorporated herein by reference in its entirety.

[0002] (Technical field) This application relates to the field of catalytic conversion of hydrocarbon oils, and in particular to a catalytic conversion process for converting heavy feedstocks into light olefins and low sulfur fuel oil components. [Background technology] With the rapid development of social and economic development, the concept of environmental protection is being replaced from post-pollution treatment to prevention of pollution at the source. Environmental pollution issues are receiving more and more attention, and corresponding legal regulations are becoming increasingly strict. According to the International Convention for the Prevention of Pollution from Ships of the International Maritime Organization (IMO), from January 1, 2020, ships around the world must use marine fuel with a sulfur content of 0.5% or less. According to BP forecast, the global consumption of marine fuel in 2020 may reach about 300 million tons. Marine fuel may pose a great challenge to the global fuel market and major oil processing companies.

[0003] Meanwhile, the problem of crude oil becoming heavier and degrading is occurring all over the world. It is estimated that heavy crude oil reserves will account for about 50% of the world's recoverable crude oil reserves after 2020. The price gap between low-quality and high-quality crude oil is widening, and the problem of how to efficiently utilize and process low-quality heavy oil to produce high-value products, improve yields, and produce low-sulfur marine fuel that meets higher environmental protection requirements has become an urgent issue facing refineries and suppliers. It is also a problem for traditional crude oil processing technologies.

[0004] CN102746890A discloses a method for producing marine fuel, in which crude oil is visbroken and fractionated to obtain a visbroken blended component. This method can reduce the production cost of marine fuel. The method includes the steps of 1) visbreaking a heavy oil component, 2) fractionating the visbroken product to collect a fraction with a high distillation range, and 3) blending the fraction with a light oil component to obtain marine fuel.

[0005] Since the price of marine fuel is lower than that of diesel oil for vehicles, it is difficult to provide good economic profit in the production of marine fuel. Therefore, it is important to produce marine fuel while producing high-value products such as propylene by a method for producing light olefins in high yield while paying attention to the component characteristics of raw oil.

[0006] Therefore, in view of the deterioration of oil quality and strict environmental protection requirements around the world, there is a need to develop a process for producing high-yield, high-value propylene while producing low-sulfur marine fuel components, so as to meet the demand for high-quality fuel oil and improve the economic profits of companies. Summary of the Invention The objective of the present application is to provide a method for producing propylene and low-sulfur fuel oil components from heavy oil. The method enables the conversion of saturated hydrocarbons in heavy feedstock oil to propylene, and the conversion of polycyclic aromatic compounds containing aromatic core structures into fuel oil components, thereby eliminating the use of saturated hydrocarbons in the fuel oil components. Therefore, the method has better economic and social benefits.

[0007] In order to achieve the above object, the present application provides a method for producing propylene and a low sulfur fuel oil component, comprising the steps of: (1) contacting a heavy feedstock oil with an extraction and separation solvent to obtain deasphalted oil and deoiled asphalt; (2) contacting the deasphalted oil and optionally a light feedstock with a catalytic conversion catalyst in the absence of hydrogen for reacting in a catalytic conversion reactor to obtain a reaction product comprising propylene; (3) separating the reaction product obtained in step (2) to obtain a catalytically cracked distillate, the catalytically cracked distillate having an initial boiling point of about 200° C. or more, a final boiling point of about 550° C. or less, and a hydrogen content of about 12.0 wt.% or less; (4) subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low sulfur hydrodistillate oil; The low sulfur hydrodistillate oil and / or the deoiled asphalt are suitable for use as a fuel oil component; wherein the catalytic conversion catalyst used in the step (2) contains about 1 to 50% by weight of zeolite, about 5 to 99% by weight of inorganic oxide, and about 0 to 70% by weight of clay, based on the total weight of the catalyst; The reaction conditions in step (2) are a reaction temperature of about 460 to 750°C, preferably about 480 to 700°C; and a weight hourly space velocity of about 10 to 100 h -1 , preferably about 30 to 100 hours -1 or the reaction time is about 1-10 seconds, preferably about 2-8 seconds; and the weight ratio of catalyst to oil is about 4-20, preferably about 5-12.

[0008] In the method of the present application, after the asphalt and resin are separated from the heavy feedstock oil by solvent deasphalting, the deoiled asphalt can be used as a fuel oil component, and the deasphalted oil is used as a feedstock for selective catalytic cracking. As a result, propylene and catalytic cracking distillate oil containing short side chain polycyclic aromatics can be obtained to the maximum extent. The catalytic cracking distillate oil can be used as a fuel oil component alone or mixed with the deoiled asphalt or heavy deasphalted oil. By using the method of the present application, the heavy feedstock oil can be converted into propylene, butylene and fuel components while significantly reducing the yield of dry gas and coke. As a result, the petroleum resources can be effectively utilized.

[0009] In particular, when compared with the prior art, the method of the present application can provide at least one of the following advantages: 1. Propylene, a valuable product, can be produced in high yields from heavy feedstock oil along with fuel oil components. By using the method, it is possible to produce about 5-20% by weight of propylene and about 30-80% by weight of fuel oil components based on the weight of the feedstock oil (heavy feedstock oil + light feedstock oil). Therefore, a more economical benefit can be obtained compared to simply using the feedstock oil to blend the fuel oil; 2. It can significantly reduce the yield of dry gas and coke while significantly increasing the production of high-value products such as propylene; 3. Virtually no slurry oil is discharged, so the total liquid yield can be significantly increased. As a result, the utilization efficiency of oil resources can be improved; 4. The catalytic conversion unit is integrated with the solvent deasphalting unit. And the properties of the catalytic cracking distillate oil obtained from the catalytic conversion unit can be changed by adjusting the solvent used in the solvent deasphalting unit and the amount of light feedstock used. As a result, this method is applicable to various amounts of heavy feedstock and fuel oil components.

[0010] BRIEF DESCRIPTION OF THE DRAWINGS The drawings that form part of this specification are provided to aid in the understanding of the present application and should not be construed as limiting the present application, which may be read with reference to the drawings in combination with the following detailed description.

[0011] FIG. 1 shows a schematic flow diagram of a preferred embodiment of the method according to the present application; FIG. 2 shows a schematic flow diagram of another preferred embodiment of the method according to the present application; FIG. 3 shows a schematic diagram of a preferred embodiment of a solvent deasphalting unit used in this application; FIG. 4 shows a schematic diagram of a preferred embodiment of the catalytic conversion unit used in this application. Detailed Disclosure of the Invention The present application will now be described in more detail with reference to specific embodiments and the accompanying drawings, which are provided for illustrative purposes only and are not intended to be limiting in any manner.

[0012] Any specific numerical value, including the end point of a numerical range, described herein is not limited to that exact numerical value. However, it should be interpreted as further including all values ​​close to the exact value, such as, for example, all values ​​within ±5% of the exact value. Furthermore, any numerical range described herein can be arbitrarily combined between the end points of the range, between each end point and any particular value within the range, or between any two particular values ​​within the range, to provide one or more new numerical ranges. The new numerical ranges are also considered to be specifically described in this application.

[0013] Unless otherwise specified, terms used herein have the same meaning as commonly understood by those of ordinary skill in the art. Where a term is defined herein and the definition of the term differs from that commonly understood in the art, the definition provided herein shall take precedence.

[0014] According to the present application, the term "catalytic cracking distillate oil" refers to a fraction in the product of catalytic conventional reaction having an initial boiling point of about 200°C or higher, preferably about 250°C or higher, and a final boiling point of about 550°C or lower, preferably about 520°C or lower, and most preferably about 500°C or lower, i.e., a fraction having a distillation range of about 200 to 550°C, preferably about 250 to 520°C, and more preferably about 250 to 500°C.

[0015] In this application, the term "fluidized bed reactor" (also described as "fluidized reactor") should be understood in the broadest sense to encompass all types of reactors that allow contact of a gaseous feedstock with solid catalyst particles in a fluidized state for chemical reaction therein. The term "fluidized bed reactor" includes, but is not limited to, dense phase beds, bubbling beds, ebullated beds, turbulent beds, high velocity beds, gas phase transport beds (e.g., upflow fluidized beds and downflow fluidized beds, etc.). The fluidized bed reactor may be a constant linear velocity fluidized bed reactor, an equal diameter fluidized bed reactor, a variable-diameter fluidized bed reactor, etc., or a composite reactor containing two or more different types of fluidized beds connected in series or parallel, such as a riser reactor or a composite reactor containing a riser reactor combined with a dense phase bed. Typically, the gas velocity of the dense phase bed may range from about 0.1 to 2 m / s, while the gas velocity of the riser reactor may range from about 1 to 30 m / s (excluding catalyst).

[0016] In the content of this application, in addition to the matters stated, any matters not stated shall be deemed to be the same as those known in the art without any modification. In addition, any embodiment described in this specification can be freely combined with one or more other embodiments described in this specification, and the technical solution or technical idea obtained thereby shall be deemed to be part of the original disclosure or original description of this specification, and shall not be deemed to be a new matter not described in this specification or unexpected, unless it is clear to a person skilled in the art that the combination is obviously inappropriate.

[0017] All patent and non-patent literature cited herein, including but not limited to textbooks and journal articles, are hereby incorporated by reference in their entirety.

[0018] As mentioned above, the present application provides a method for producing propylene and fuel oil components, comprising the steps of: (1) A step of contacting a heavy feedstock oil with an extraction and separation solvent to obtain a deasphalted oil and a deoiled asphalt; (2) contacting the deasphalted oil and optionally a light feedstock with a catalytic conversion catalyst in the absence of hydrogen for reacting in a catalytic conversion reactor to obtain a reaction product comprising propylene; (3) separating the reaction product obtained in step (2) to obtain a catalytically cracked distillate oil, and optionally a liquefied gas containing propylene and gasoline; (4) subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low sulfur hydrodistillate oil; Here, the low sulfur hydrodistillate and / or deoiled asphalt can be used as the fuel oil component.

[0019] According to the present application, step (1) is a solvent deasphalting step. Step (1) can be carried out in one or two stages. In a particular preferred embodiment, step (1) is carried out in two stages to obtain light deasphalted oil, heavy deasphalted oil, and deoiled asphalt. Here, the light deasphalted oil is used as a feedstock for catalytic conversion step (2). Also, the heavy deasphalted oil can be used as a fuel oil component or for other purposes. Furthermore, the deoiled asphalt can be used as a fuel oil component or asphalt for roads, depending on its sulfur content.

[0020] In the present application, the heavy feedstock used in step (1) may be any heavy oil suitable for use in a catalytic conversion process, for example, selected from vacuum residue, inferior atmospheric residue, hydrotreated heavy oil, or any mixture thereof.

[0021] In the present application, the solvent used in step (1) can be any solvent suitable for use in the solvent deasphalting of heavy oil. The solvent can be selected from, for example, lower alkanes such as propane, butane, pentane, or any mixture thereof. The deasphalting solvent can also be selected according to the properties of the catalytic cracking distillate oil obtained from the catalytic conversion unit.

[0022] In a preferred embodiment, the conditions for the solvent deasphalting step (1) may include the following: a reaction temperature of about 10 to 200°C, preferably about 20 to 180°C, a reaction pressure of about 1.0 to 15.0 MPa, preferably about 2.0 to 10.0 MPa, and a mass ratio of the solvent to the heavy feedstock oil (also referred to as the "solvent ratio") of about 1 to 20, preferably about 3 to 10.

[0023] According to the present application, the light feedstock oil used in step (2) may be selected from the group consisting of petroleum hydrocarbons, other mineral oils, or mixtures thereof. The petroleum hydrocarbons may be selected from the group consisting of vacuum gas oil, atmospheric gas oil, coker gas oil, high-quality residual oil, high-quality hydrogenated heavy oil, or any mixtures thereof. The other mineral oils may be selected from the group consisting of coal liquid oil, tar sand oil, shale oil, or any mixtures thereof. The "high-quality residual" and "high-quality hydrogenated heavy oil" refer to residual oil and hydrogenated heavy oil, respectively, having a hydrogen content of 11.2% or more, preferably 12.0% or more, and most preferably 12.5% ​​or more.

[0024] According to the present application, the catalytic conversion reactor used in step (2) can be selected from various types of fluidized bed reactors, such as a single fluidized bed reactor, or a composite reactor including multiple fluidized bed reactors connected in series or parallel. In certain preferred embodiments, the fluidized bed reactor may be an isodiameter riser reactor, such as the reactor disclosed in Chinese Patent No. 1078094C, or various types of variable diameter fluidized bed reactors.

[0025] According to the present application, the catalytic conversion catalyst used in step (2) can contain, based on the total weight of the catalyst, about 1-50% by weight of zeolite, about 5-99% by weight of inorganic oxide, and about 0-70% by weight of clay. Preferably, the catalyst contains about 5-45% by weight of zeolite, more preferably about 10-40% by weight of zeolite, about 5-80% by weight of inorganic oxide, and about 10-70% by weight of clay.

[0026] In a preferred embodiment, the zeolite may comprise about 51-100 wt%, preferably about 70-100 wt%, of mesoporous zeolite and about 0-49 wt%, preferably about 0-30 wt%, of macroporous zeolite, based on the total weight of the zeolite. Preferably, the mesoporous zeolite has a silica-alumina ratio of more than about 10, preferably more than about 50, more preferably more than about 100. The mesoporous zeolite is preferably selected from the group consisting of ZSM-type zeolite and ZRP-type zeolite, and the macroporous zeolite is preferably a Y-type zeolite. Optionally, the zeolite may be modified with non-metallic elements such as phosphorus, and / or transition metal elements such as iron, cobalt, nickel. The inorganic oxide is preferably selected from the group consisting of silica, alumina, and combinations thereof, and the clay is preferably selected from kaolin and / or halloysite.

[0027] According to the present application, step (2) is carried out under effective conditions. The term "effective conditions" refers to conditions that allow the reaction feedstock to undergo a catalytic conversion reaction to obtain a reaction product containing propylene and catalytic cracking distillate oil (preferably containing about 8-25 wt. % propylene and about 15-50 wt. % catalytic cracking distillate oil) based on the weight of the reaction feedstock itself (i.e., deasphalted oil + any light feedstock oil). In a preferred embodiment, the reaction conditions in step (2) include the following conditions: a reaction temperature of about 460-750°C, preferably about 480-700°C, more preferably about 480-600°C, and most preferably about 500-560°C; (e.g., in the case of a dense phase bed reactor, a fast bed reactor, etc.) a weight hourly space velocity of about 5-100 h -1 , preferably about 10 to 70 hours -1 , more preferably about 15 to 50 hours -1 , and most preferably about 18 to 40 hours -1or (e.g., in the case of a riser reactor) a reaction time of about 1 to 10 seconds, preferably about 2 to 8 seconds, more preferably about 2.5 to 8 seconds, and most preferably about 3 to 8 seconds; the weight ratio of catalytic conversion catalyst to the feed oil to be catalytically converted (also referred to as the "weight ratio of catalyst to oil" or "catalyst to oil ratio") is about 4 to 20, preferably about 5 to 12, preferably about 5 to 10, and more preferably about 5 to 9.

[0028] In a preferred embodiment, step (2) is carried out so that the resulting reaction product has a propylene / propane mass ratio of greater than or equal to about 4, preferably greater than or equal to about 6, and most preferably greater than or equal to about 8; and / or an isobutene / isobutane mass ratio of greater than or equal to about 1, preferably greater than or equal to about 1.5, and most preferably greater than or equal to about 1.8.

[0029] In a preferred embodiment, step (2) is carried out so that the yield of catalytically cracked distillate oil in the resulting reaction product, i.e., the weight ratio of catalytically cracked distillate oil to the feedstock oil for the catalytic conversion reaction (i.e., deasphalted oil and any light feedstock oil), is about 15% or more, preferably about 20% or more, more preferably about 30% or more, and about 50% or less.

[0030] As known to those skilled in the art, the conversion rate of feedstock in a catalytic conversion process is typically expressed as the sum of the yields of gas, gasoline and coke. In the process of the present application, the final products of the catalytic conversion process only include dry gas, liquefied gas, gasoline, catalytic cracked distillate and coke. Therefore, in the present application, the conversion rate of feedstock is substantially 100% after subtracting the yield of catalytic cracked distillate. The conversion rate of the catalytic conversion process according to the present application is then controlled to a level of about 85% or less, preferably about 80% or less, most preferably about 70% or less and about 50% or more.

[0031] In a particularly preferred embodiment, the method further comprises a step of separating the reaction product of step (2) from the spent catalyst. The spent catalyst is stripped and regenerated by burning coke, and then recycled to the reactor. The separated reaction product of step (2) comprises propylene, gasoline, and catalytic cracking distillate. Methods for separating materials such as propylene from the reaction product are well known to those skilled in the art, and methods for solvent deasphalting of heavy feedstocks are also well known to those skilled in the art, and therefore will not be described in detail herein.

[0032] According to the present application, the catalytically cracked distillate oil obtained in step (3) has an initial boiling point of about 200° C. or higher, a final boiling point of about 550° C. or lower, and a hydrogen content of about 12.0% by weight or lower. Preferably, the catalytically cracked distillate oil has an initial boiling point of about 250° C. or higher, a final boiling point of about 520° C. or lower, more preferably 500° C. or lower, and a hydrogen content of about 11.0% by weight or lower.

[0033] According to the present application, the fuel oil component can be optionally formed by mixing the hydrodesulfurized catalytically cracked distillate oil with the deoiled asphalt or heavy deasphalted oil obtained in a solvent deasphalting unit.

[0034] According to the present application, the catalyst used in the hydrodesulfurization step (4) is a catalyst comprising a group VIB metal and / or a group VIII metal, preferably supported on an alumina and / or amorphous silica-alumina support. More preferably, the catalyst used in the hydrotreating step (4) comprises about 0-10% by weight of additive, about 1-40% by weight of at least one group VIII metal (calculated as metal oxide), and about 1-50% by weight of at least one group VIB metal (calculated as metal oxide), the remainder being a support selected from alumina and amorphous silica-alumina, the additive comprising a non-metallic element selected from fluorine, phosphorus, etc., a metallic element selected from titanium, platinum, etc., or a combination thereof. For example, the additive may be a phosphorus-containing auxiliary or a fluorine-containing auxiliary such as ammonium fluoride. The group VIB metal is preferably selected from molybdenum, tungsten, or a combination thereof, and the group VIII metal is preferably selected from nickel, cobalt, or a combination thereof.

[0035] In a preferred embodiment, the hydrodesulfurization step (4) comprises the following conditions: a reaction pressure of about 2.0 to 24.0 MPa, preferably about 3.0 to 15 MPa; a reaction temperature of about 200 to 500° C., preferably about 300 to 400° C.; a volume ratio of hydrogen to oil of about 50 to 5000 N. 3 / m 3 , preferably about 200 to 2000 N 3 / m 3 Liquid hourly space velocity is about 0.1 to 30.0 h -1 , preferably about 0.2 to 10.0 h -1 .

[0036] In a preferred embodiment, the sulfur content of the low sulfur hydrodistillate obtained in step (4) via hydrodesulfurization of the catalytically cracked distillate is about 0.1% or less, preferably about 0.05% or less.

[0037] In a particularly preferred embodiment, the method of the present application comprises the steps of: (1) contacting a heavy feedstock oil with a solvent in a one-stage solvent deasphalting unit to extract and separate the heavy feedstock oil and deoiled asphalt; (2) contacting the deasphalted oil and optionally the light feedstock with a catalytic conversion catalyst for reacting in a catalytic conversion reactor in the absence of hydrogen to obtain a reaction product comprising propylene; (3) separating the reaction product obtained in step (2) to obtain a liquefied gas containing dry gas, propylene, gasoline and catalytic cracking distillate, and the liquefied gas can be further separated to obtain propylene, propane and C4 hydrocarbons; (4) subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low-sulfur hydrodistillate oil; Wherein the low sulfur hydrodistillate oil can be used alone as a fuel oil component or can be mixed with deoiled asphalt and then used as a fuel oil component; Preferably, the low sulfur hydrodistillate oil is blended with the deoiled asphalt to form a fuel oil component or product.

[0038] In another particularly preferred embodiment, the method according to the present application comprises the steps of: (1) contacting a heavy feedstock with a solvent in a two-stage solvent deasphalting unit to extract and separate light deasphalted oil, heavy deasphalted oil and deoiled asphalt; (2) contacting and reacting the light deasphalted oil and, optionally, the light feedstock oil with a catalytic conversion catalyst in the absence of hydrogen in a catalytic conversion reactor to obtain a reaction product containing propylene; (3) separating the reaction product from step (2) to obtain a liquefied gas comprising dry gas, propylene, gasoline and catalytically cracked distillate, wherein the liquefied gas can be further separated to obtain propylene, propane and C4 hydrocarbons;

[0039] (4) subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low-sulfur hydrodistillate oil; Wherein the low sulfur hydrodistillate oil can be used alone as a fuel oil component or can be mixed with heavy deasphalted oil or deoiled asphalt and then used as a fuel oil component; Preferably, the low sulfur hydrodistillate oil is blended with heavy deasphalted oil to form a fuel oil component or product.

[0040] A preferred embodiment of the method according to the present application will now be described with reference to the drawings.

[0041] In a particularly preferred embodiment, as shown in FIG. 1, a heavy feedstock is fed via pipeline 1″ to a single-stage solvent deasphalting unit 2″ for contact with a solvent (not shown) and separation to obtain a deasphalted oil and a deoiled asphalt. The deoiled asphalt is discharged via pipeline 4″ and the solvent is recycled (not shown). The deasphalted oil is optionally mixed with a light feedstock from pipeline 5″ and then sent via pipeline 3″ to a catalytic conversion unit 6″ for contacting and reacting with a catalytic conversion catalyst. After separation of catalytic conversion products, the resulting dry gas is discharged through pipeline 7"; the resulting liquefied gas is recovered through pipeline 8" and further separated into propylene, propane and C4 hydrocarbons; the resulting gasoline is discharged through pipeline 9"; the resulting catalytic cracked distillate is recovered through pipeline 10" and subjected to hydrodesulfurization treatment in hydrodesulfurization unit 11". The hydrocatalytic cracked distillate is recovered as a fuel oil component through pipeline 12" or mixed with deoiled asphalt from pipeline 4" through pipeline 13" or, optionally, further mixed with light distillate from pipeline 15" to become a fuel oil component or product.

[0042] In another particularly preferred embodiment, as shown in FIG. 2, a heavy feedstock oil is fed via pipeline 1″ to a two-stage solvent deasphalting unit 2″ (the process scheme of the two-stage solvent deasphalting is shown diagrammatically in FIG. 3) where it is contacted with a solvent (not shown) and separated to obtain a light deasphalted oil, a heavy deasphalted oil and a deoiled asphalt. The heavy deasphalted oil and the deoiled asphalt are discharged via pipelines 14″ and 4″, respectively, and the solvent is recycled (not shown). The light deasphalted oil is optionally mixed with light feedstock oil from pipeline 5" and then sent through pipeline 3" to catalytic conversion unit 6" to contact and react with catalytic conversion catalyst. After separation of catalytic conversion products, the resulting dry gas is discharged through pipeline 7"; the resulting liquefied gas is recovered through pipeline 8" and can be further separated into propylene, propane and C4 hydrocarbons; the resulting gasoline is discharged through pipeline 9"; the resulting catalytic cracked distillate is recovered through pipeline 10" and subjected to hydrodesulfurization treatment in hydrodesulfurization unit 11"; the hydrocatalytic cracked distillate is recovered as a fuel oil component through pipeline 12" or mixed with heavy deasphalted oil from pipeline 14" through pipeline 13" to be a fuel oil component or product.

[0043] FIG. 3 shows a two-stage solvent deasphalting process in which the feedstock oil is fed to the extraction tower I of the deasphalting unit through pipeline 1' and separated by contact with the solvent from pipeline 2' to obtain deasphalted oil and deasphalted oil containing the solvent. The deoiled asphalt containing the solvent is sent to the asphalt evaporator through pipeline 5' for separation, the obtained deoiled asphalt is discharged through pipeline 11' and the solvent is discharged through pipeline 8'. The deasphalted oil is sent to the extraction tower II through pipeline 3' and separated by contact with the solvent from pipeline 4' to obtain light deasphalted oil and heavy deasphalted oil. The light deasphalted oil is sent through pipeline 6' to a light oil evaporator for separation, the solvent is discharged through pipeline 8', the light deasphalted oil is discharged through pipeline 9', the heavy deasphalted oil is sent through pipeline 7' to a heavy oil evaporator for separation, the solvent is discharged through pipeline 8', and the heavy deasphalted oil is discharged through pipeline 10'.

[0044] As shown in FIG. 4, in a particularly preferred embodiment, a pre-lifting medium is injected into the bottom of a variable diameter fluidized bed reactor 2 (such as the reactor disclosed in China Patent No. 1078094C) through a pipeline 1, and the regenerated catalyst from a regenerated catalyst inclined pipe 16 is moved upward along the reactor under the action of the pre-lifting medium. Light deasphalted oil from a pipeline 9' is fed into the bottom of the first reaction zone 8 of the variable diameter fluidized bed reactor 2 through a pipeline 3 together with atomized steam from a pipeline 4, and mixed with the stream present in the reactor. The feed oil is cracked on the high temperature catalyst and moved upward to the second reaction zone 9 of the variable diameter fluidized bed reactor 2 for further reaction. The obtained oil gas and the deactivated spent catalyst are passed through a cyclone separator in a disengager 7 to separate the spent catalyst from the oil gas. The oil gas is passed through a main oil gas pipeline 17, and the catalyst fines are returned to the separator 7 through the dipleg of the cyclone separator. The spent catalyst in the separator 7 is sent to the stripping section 10 to be contacted with the stripped steam from the pipeline 11. The oil and gas removed from the spent catalyst passes through a cyclone separator and is sent to the main oil and gas pipeline 17. After the removed spent catalyst is sent to the regenerator 13 through the spent catalyst inclined pipe 12, main air is introduced into the regenerator through the pipeline 14 to burn the coke deposited on the spent catalyst. As a result, the deactivated spent catalyst can be regenerated. The exhaust gas is discharged through the pipeline 15. The regenerated catalyst is recirculated to the variable diameter fluidized bed reactor 2 through the regenerated catalyst inclined pipe 16 and reused.

[0045] The oil gas is sent through the main oil gas pipeline 17 to the next fractionation unit 18, and after separation, the obtained dry gas is discharged through the pipeline 19. The obtained liquefied gas is discharged through the pipeline 20 and separated into propylene, propane and C4 hydrocarbons in the gas separation unit 25, and the propylene, propane and C4 hydrocarbons are discharged through the pipelines 26, 27 and 28, respectively. The obtained gasoline is discharged through the pipeline 21. The obtained light cycle oil fraction having a distillation range of 200-250 ° C is recovered through the pipeline 22, and then recycled through the pipeline 31 together with the atomized steam from the pipeline 32 to the central upper part of the first reaction zone 8 of the variable diameter fluidized bed reactor 2. The obtained slurry oil is recovered through the pipeline 24 and recycled to the first reaction zone 8 of the variable diameter fluidized bed reactor 2 for purification (optionally passed through the feed nozzle to the first reaction zone 8 together with the feed oil from the pipeline 3), and the fine powder of the catalyst is recovered. The resulting catalytic cracking distillate is sent to the hydrotreating unit 29 through the pipeline 23. The hydrotreating distillate obtained after hydrotreating is taken out through the pipeline 30 together with the heavy deasphalted oil from the pipeline 10' as a blending component for marine fuel. The distillation range and process scheme of each fraction can be adjusted according to the actual needs of the refinery. For example, gasoline can be separated to obtain a light gasoline fraction, and the light gasoline fraction can be recycled through the pipeline 6 together with the atomized steam from the pipeline 5 to the second reaction zone 9 of the variable diameter fluidized bed reactor 2 to increase the yield of propylene by refining.

[0046] In certain preferred embodiments, the present application provides the following technical solutions: 1. A method for producing more propylene and low sulfur fuel oil components, comprising the steps of: (1) contacting a heavy feedstock oil with an extraction and separation solvent to obtain a deasphalted oil and a deoiled asphalt; (2) feeding the deasphalted oil and optionally a light feedstock oil into a catalytic conversion reactor as catalytic conversion feedstock oils and contacting them with a catalytic conversion catalyst for reaction to obtain a liquefied gas containing propylene, gasoline and catalytic cracking distillate oil; (3) subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low-sulfur hydrodistillate oil; Here, the low sulfur hydrodistillate oil and / or the deoiled asphalt are used as a fuel oil component.

[0047] 2. The method of claim 1, wherein the heavy feedstock is selected from the group consisting of vacuum residue, inferior atmospheric residue, hydrotreated heavy oil, or a mixture of two or more thereof.

[0048] 3. The method according to item 1, wherein the solvent is selected from a lower alkane, or a mixture of two or more thereof, and the lower alkane is selected from the group consisting of propane, butane and pentane, or a mixture of two or more thereof.

[0049] 4. The method according to item 1, wherein the step (1) is carried out at an operating temperature of 10 to 200°C, preferably 20 to 180°C, an operating pressure of 1.0 to 15.0 MPa, preferably 2.0 to 10.0 MPa, and a mass ratio of the solvent to the feedstock oil of 1 to 20, preferably 3 to 10.

[0050] 5. The method according to item 1, wherein the light feedstock oil used in step (2) is selected from petroleum hydrocarbons and / or other mineral oils, the petroleum hydrocarbons are selected from the group consisting of vacuum gas oil, atmospheric gas oil, coker gas oil, high-quality residual oil, high-quality hydrogenated heavy oil, or a mixture of two or more thereof, and the other mineral oils are selected from the group consisting of coal liquid oil, tar sands oil, shale oil, or a mixture of two or more thereof.

[0051] 6. The method according to item 1, wherein in step (2), the reactor is selected from the group consisting of a riser reactor, a constant linear velocity fluidized bed, an equal diameter fluidized bed, an upflow conveyor line, a downflow conveyor line, a combination of two or more of these, or a combination of reactors connected in series and / or in parallel, and the riser reactor is a conventional equal diameter riser reactor or various types of variable diameter fluidized beds.

[0052] 7. The method according to item 1, wherein the catalytic conversion catalyst used in step (2) comprises 1-50% by weight of zeolite, 5-99% by weight of inorganic oxide and 0-70% by weight of clay, based on the total weight of the catalyst, wherein the zeolite is a mesoporous zeolite and optionally a macroporous zeolite, the mesoporous zeolite accounts for 51-100% by weight of the total weight of the zeolite, the mesoporous zeolite has a silica-alumina ratio of more than 50, preferably more than 80, and the macroporous zeolite accounts for 0-49% by weight of the total weight of the zeolite.

[0053] 8. The conditions for the catalytic conversion in the step (2) are a reaction temperature of 460 to 750°C, preferably 480 to 700°C, and a weight hourly space velocity of 10 to 100 h -1 , preferably 30 to 80 hours -1 and the weight ratio of the catalyst to the catalytic conversion feedstock oil is 4-20, preferably 5-12.

[0054] 9. The method according to item 1, wherein the catalytic cracking distillate oil obtained in the step (2) has an initial boiling point of 200° C. or higher and a hydrogen content of 12.0% by weight or less.

[0055] 10. The method according to item 9, wherein the catalytic cracking distillate oil has an initial boiling point of 250° C. or higher and a hydrogen content of 11.0% by weight or less.

[0056] 11. The process according to item 1, wherein the catalyst used in the hydrodesulfurization step (3) is a catalyst comprising a Group VIB metal and / or a Group VIII metal supported on an alumina and / or an amorphous silica-alumina support.

[0057] 12. The method according to item 11, wherein the hydrotreating catalyst comprises 0-10 wt. % of an additive, 1-40 wt. % of one or more Group VIII metals, 1-50 wt. % of one or more Group VIB metals, and the balance alumina and / or amorphous silica-alumina support, and the additive is selected from the group consisting of non-metallic elements such as fluorine, phosphorus, and metallic elements such as titanium, platinum, and the like.

[0058] 13. The conditions of the hydrodesulfurization are: reaction pressure 2.0-24.0 MPa, reaction temperature 200-500°C, volume ratio of hydrogen to oil 50-5000 Nm 3 / m 3 , and liquid hourly space velocity is 0.1 to 30.0 h -1 2. The method according to claim 1, comprising:

[0059] 14. The hydrodesulfurization conditions are: reaction pressure 3.0-15.0 MPa, reaction temperature 300-400°C, volume ratio of hydrogen to oil 200-2000 Nm 3 / m 3 , and liquid hourly space velocity is 0.2 to 10.0 h -1 14. The method according to claim 13, comprising:

[0060] 15. The method according to item 1, wherein the sulfur content of the hydrodistilled oil obtained in step (3) is 0.1% or less, preferably 0.05% or less.

[0061] [Example] The present application will be further described with reference to the following examples, but the present application is not limited thereto.

[0062] The characteristics of the feedstock oil and catalyst used in the following Examples and Comparative Examples are shown in Tables 1 and 2, respectively. In the Comparative Examples, MMC-1, a catalyst manufactured by Kilbranch of Sinopec Catalyst Co., Ltd., was used as the catalytic conversion catalyst.

[0063] The hydrogen content of the catalytically cracked distillate oil obtained in each example was measured using a carbon and hydrogen analyzer in accordance with the NB / SH / T 0656-2017 standard.

[0064] The catalyst used in this example was prepared as follows: 969g of halloysite (purchased from China Kaolin Clay Co., Ltd., solid content 73%) was slurried in 4300g of decationized water, 781g of pseudoboehmite (with solid content of 64%, purchased from Shandong Zibo Bauxite Plant) and 144ml of hydrochloric acid (concentration 30%, specific gravity 1.56) were added and stirred uniformly. The mixture was allowed to stand and aged at 60°C for 1 hour to keep the pH at 2-4, and then the mixture was cooled to room temperature. 5000g of pre-prepared slurry containing chemical water and 1600g of mesopore shape-selective ZSM-5 zeolite with silica-alumina ratio above 150 (purchased from Sinopec Catalyst Co., Ltd. Qilu Branch) was added, stirred uniformly, spray-dried, and free Na was added. + The catalyst was then washed away to obtain a catalyst. The obtained catalyst was aged at 800°C with 100% steam, and the aged catalyst was designated as catalyst A. The properties of catalyst A are shown in Table 2.

[0065] The hydrodesulfurization catalyst B used in the examples was prepared as follows: 1000g of pseudo-boehmite manufactured by ChangLing Branch of Sinopec Catalyst Co., Ltd. was weighed out, and then 1000ml of an aqueous solution containing 10ml of nitric acid (chemically pure) was added. The resulting mixture was formed into a band shape by band extrusion using a twin-screw extruder, dried at 120°C for 4 hours, and calcined at 800°C for 4 hours to obtain a catalyst support. The resulting support was immersed in 900ml of an aqueous solution containing 120g of ammonium fluoride for 2 hours, dried at 120°C for 3 hours, and calcined at 600°C for 3 hours. After cooling to room temperature, the resultant was further immersed in 950ml of an aqueous solution containing 133g of ammonium metamolybdate for 3 hours, dried at 120°C for 3 hours, and calcined at 600°C for 3 hours. After cooling to room temperature again, the resultant was finally immersed in 900 ml of an aqueous solution containing 180 g of nickel nitrate and 320 g of ammonium metatungstate for 4 hours, dried at 120° C. for 3 hours, and calcined at 600° C. for 4 hours to obtain catalyst B.

[0066] [Table 1]

[0067] [Table 2]

[0068] (Example 1-a) This example was carried out using vacuum residue VR-1 as heavy feedstock oil according to the process scheme shown in Figure 1. The properties of the deasphalted oil and deoiled asphalt obtained by solvent deasphalting the heavy feedstock oil with propane are shown in Table 3.

[0069] Using catalyst A as a catalytic conversion catalyst, a test was carried out using a medium-sized catalytic cracking unit containing a variable diameter fluidized bed reactor containing 100% propane-deasphalted oil. The resulting oil-gas and spent catalyst were separated in a separator, and the oil-gas products were divided into propylene, butylene, gasoline and catalytic cracking distillate oil (distillation range 250-500°C, hydrogen content 9.4 wt%) according to the distillation range of each fraction by a fractionator. The reaction conditions and product distribution are shown in Table 4.

[0070] The resulting catalytic cracking distillate oil was sent to a hydrodesulfurization reactor together with hydrogen, and contacted with hydrodesulfurization catalyst B. The reaction pressure was 6.0 MPa, the reaction temperature was 350°C, the volume ratio of hydrogen to oil was 350, and the liquid hourly space velocity was 2.0 h -1 The resulting low-sulfur hydrodistillate was used as a fuel oil component and mixed with the second fuel oil component (i.e., the deoiled asphalt obtained in this example) and the third fuel oil component, i.e., hydrogenated diesel oil, to obtain RMG 180 fuel oil products that meet the national marine fuel oil standard GB 17411-2015. The properties of these fuel oil products are shown in Table 5.

[0071] (Example 1-b) This example was carried out as described in Example 1, except that a medium-sized catalytic cracking unit containing an isodiameter riser reactor was used instead of a medium-sized catalytic cracking unit containing a variable diameter fluidized bed reactor. The resulting oil-gas and spent catalyst were separated in a separator, and the oil-gas product was divided into propylene, butylene, gasoline and catalytic cracking distillate (distillation range 250-500°C, hydrogen content 9.4 wt%) according to the distillation range of each fraction by a fractionator. The reaction conditions and product distribution are shown in Table 4.

[0072] Example 2 This example was carried out using vacuum residue VR-1 as heavy feedstock oil, according to the process scheme shown in Figure 1. The properties of the deasphalted oil and deoiled asphalt obtained by solvent deasphalting the heavy feedstock oil with butane are shown in Table 3.

[0073] Using catalyst A as a catalytic conversion catalyst, a test was carried out using a medium-sized catalytic cracking unit containing a variable diameter fluidized bed reactor containing a mixture of 80% butane deasphalted oil and 20% VGO. The resulting oil-gas and spent catalyst were separated in a separator, and the oil-gas products were divided into propylene, butylene, gasoline, and catalytic cracking distillate (distillation range 250-500°C, hydrogen content 10.1 wt%) according to the distillation range of each fraction by a fractionator. The reaction conditions and product distribution are shown in Table 4.

[0074] The resulting catalytic cracking distillate oil was sent to a hydrodesulfurization reactor together with hydrogen, where it was brought into contact with hydrodesulfurization catalyst B. The reaction pressure was 7.0 MPa, the reaction temperature was 380°C, the volume ratio of hydrogen to oil was 500, and the liquid hourly space velocity was 1.5 h -1 The low sulfur hydrodistillate was reacted with the deoiled asphalt obtained in this example to obtain a low sulfur hydrodistillate. The low sulfur hydrodistillate was used as a fuel oil component and mixed with another fuel oil component (i.e., the deoiled asphalt obtained in this example) to obtain a RMG 380 fuel oil product that meets the national marine fuel oil standard GB 17411-2015. The properties of the obtained fuel oil product are shown in Table 6.

[0075] Example 3 This example was carried out using vacuum residue VR-1 as heavy feedstock oil according to the process scheme shown in Figure 1. The heavy feedstock oil was subjected to solvent deasphalting with pentane, and the properties of the resulting deasphalted oil and deoiled asphalt are shown in Table 3.

[0076] Using catalyst A as a catalytic conversion catalyst, a test was carried out using a medium-sized catalytic cracking unit containing a variable diameter fluidized bed reactor with a mixture of 60% pentane deasphalted oil and 40% VGO. The resulting oil-gas and spent catalyst were separated in a separator, and the oil-gas products were divided into propylene, butylene, gasoline and catalytic cracking distillate oil (distillation range 250-500°C, hydrogen content 10.4 wt%) according to the distillation range of each fraction by a fractionation unit. The reaction conditions and product distribution are shown in Table 4.

[0077] The resulting catalytic cracking distillate oil was sent to a hydrodesulfurization reactor together with hydrogen, where it was brought into contact with hydrodesulfurization catalyst B. The reaction pressure was 8.0 MPa, the reaction temperature was 310°C, the volume ratio of hydrogen to oil was 550, and the liquid hourly space velocity was 4.0 h -1 The low sulfur hydrodistillate was reacted with 100% ethanol to obtain a low sulfur hydrodistillate. The low sulfur hydrodistillate was used as a fuel oil component and mixed with another fuel oil component (i.e., the deoiled asphalt obtained in this example) to obtain a RMG 180 fuel oil product that meets the national marine fuel standard GB 17411-2015. The properties of the obtained fuel oil are shown in Table 7.

[0078] Comparative Example 1 This comparative example was carried out on a medium-sized unit including a riser reactor combined with a dense-phase fluidized bed, using VGO as the feedstock and catalyst MMC-1 as the catalytic cracking catalyst according to the conventional deep catalytic cracking process described in CN1004878B. The resulting oil gas and spent catalyst were separated in a separator, and the products were fractionated into propylene, butylene, gasoline and light cycle oil (distillation range 200-350 °C, hydrogen content 9.8 wt%) according to the distillation range of each fraction by a fractionator. The reaction conditions and product distribution are shown in Table 4.

[0079] [Table 3]

[0080] [Table 4]

[0081] JPEG0007636405000005.jpg106169

[0082] As can be seen from the results in Table 4, Example 1-a and Example 1-b can provide not only a propylene yield of more than 5 wt%, but also a fuel oil component yield of about 70 wt% (calculated based on hydrodistillate + deoiled asphalt, with vacuum residue VR-1 used as heavy feedstock). Compared with Comparative Example 1, the dry gas yield of Example 1-a and Example 1-b is significantly decreased, and the total liquid yield is significantly increased.

[0083] [Table 5]

[0084] [Table 6]

[0085] [Table 7]

[0086] Example 4 This example was carried out using hydrogenated heavy oil as the heavy feedstock oil according to the process scheme shown in Figure 2. The heavy feedstock oil was solvent deasphalted with butane, and the properties of the light deasphalted oil, heavy deasphalted oil and deoiled asphalt are shown in Table 8.

[0087] Catalyst A was used as a catalytic conversion catalyst to carry out tests in a medium-sized catalytic cracking unit containing a variable diameter bed reactor filled with 100% light butane deasphalted oil. The resulting oily gas and spent catalyst were separated in a separator, and the oily gas products were divided into propylene, butylene, gasoline and catalytic cracking distillate oil (distillation range 250-500°C, hydrogen content 10.4 wt%) according to the distillation range of each fraction by a fractionator. The reaction conditions and product distribution are shown in Table 9.

[0088] The resulting catalytic cracking distillate oil was sent to a hydrodesulfurization reactor together with hydrogen, where it was contacted with hydrodesulfurization catalyst B. The reaction pressure was 9.0 MPa, the reaction temperature was 330°C, the volume ratio of hydrogen to oil was 650, and the liquid hourly space velocity was 8.0 h -1 The low-sulfur hydrodistillate was reacted with 100% ethanol to obtain low-sulfur hydrodistillate. The low-sulfur hydrodistillate was used as a fuel oil component and mixed with another fuel oil component "vacuum residue VR-2" to obtain RMG 180 fuel oil product, which meets the national marine fuel oil standard GB 17411-2015. The properties of the obtained fuel oil product are shown in Table 10.

[0089] Example 5 This example was carried out using hydrogenated heavy oil as the heavy feedstock oil according to the process scheme shown in Figure 2. The heavy feedstock oil was subjected to solvent deasphalting treatment with propane, and the properties of the obtained light deasphalted oil, heavy deasphalted oil and deoiled asphalt are shown in Table 8.

[0090] Using catalyst A as a catalytic conversion catalyst, the test was carried out in a medium-sized catalytic cracking unit, including a variable diameter fluidized bed reactor containing 100% light propane deasphalted oil. The resulting oil gas and spent catalyst were separated in a separator, and the oil gas product was divided into propylene, butylene, gasoline and catalytic cracking distillate oil (distillation range 250-500°C, hydrogen content 10.5 wt%) according to the distillation range of each fraction by a fractionation unit. The reaction conditions and product distribution are shown in Table 9.

[0091] The resulting catalytic cracking distillate oil was sent to a hydrodesulfurization reactor together with hydrogen, where it was brought into contact with hydrodesulfurization catalyst B. The reaction pressure was 6.0 MPa, the reaction temperature was 350°C, the volume ratio of hydrogen to oil was 350, and the liquid hourly space velocity was 4.0 h -1 The low sulfur hydrodistillate was used as a fuel oil component and blended with the second fuel oil component (i.e., the heavy deasphalted oil obtained in this example) and the third fuel oil component "vacuum residue VR-3" to obtain an RMG 380 fuel oil product that meets the national marine fuel oil standard GB 17411-2015. The properties of the obtained fuel oil product are shown in Table 11.

[0092] [Table 8]

[0093] [Table 9]

[0094] [Table 10]

[0095] [Table 11]

[0096] As can be seen from the results shown in the table above, the present process is capable of providing a high value product, propylene, while producing a quantity of fuel oil components.

[0097] The preferred embodiments of the present application have been described in detail above. However, the present application is not limited to these detailed embodiments. Various modifications can be made without departing from the spirit of the present application, and these modifications are also within the scope of the present application.

[0098] It should be noted that the various technical features described in the above embodiments can be combined as appropriate without causing any contradiction. For the sake of brevity, the various possible combinations are not separately described in this application. However, such combinations are within the scope of this application.

[0099] In addition, the various embodiments of the present application may be combined in any manner without departing from the spirit of the present application, and such combinations should be considered as part of the disclosure of the present application. [Brief description of the drawings]

[0100] [Figure 1] 1 shows a schematic flow diagram of a preferred embodiment of the method according to the present application. [Diagram 2] 1 shows a schematic flow diagram of another preferred embodiment of the method according to the present application. [Diagram 3] FIG. 1 shows a schematic diagram of a preferred embodiment of a solvent deasphalting unit used in this application. [Figure 4] FIG. 1 shows a schematic diagram of a preferred embodiment of a catalytic conversion unit used in this application.

Claims

1. 1. A process for producing propylene and a low sulfur marine fuel oil component, the process comprising: (1) contacting a heavy feedstock oil with an extraction and separation solvent to obtain a light deasphalted oil, a heavy deasphalted oil, and a deoiled asphalt; (2) contacting the light deasphalted oil and optionally the light feedstock with a catalytic conversion catalyst in the absence of hydrogen for reacting in a catalytic conversion reactor to obtain a reaction product containing propylene, and controlling the conversion rate of the catalytic conversion step to 50%-70%; (3) A step of separating the reaction product obtained in step (2) to obtain a catalytic cracking distillate oil, wherein the catalytic cracking distillate oil has an initial boiling point of 200° C. or more, a final boiling point of 550° C. or less, and a hydrogen content of 12.0 wt.% or less; (4) subjecting the catalytic cracking distillate oil to hydrodesulfurization to obtain a low sulfur hydrodistillate oil; (5) Mixing the low sulfur hydrodistillate oil with one or more fuel oil components selected from the heavy deasphalted oil, vacuum residue, and deoiled asphalt to obtain the marine fuel oil; wherein the catalytic conversion catalyst used in the step (2) comprises 1 to 50% by weight of zeolite, 5 to 99% by weight of inorganic oxide, and 0 to 70% by weight of clay, based on the total weight of the catalyst; The reaction conditions of step (2) are: reaction temperature is 460-750° C.; weight hourly space velocity is 10-100 h-1 or reaction time is 1-10 s; and weight ratio of catalyst to oil is 4-20.

2. 2. The process of claim 1, wherein the zeolite comprises 51-100 wt. % mesoporous zeolite and 0-49 wt. % macroporous zeolite, based on the total weight of zeolites in the catalytic conversion catalyst, and the mesoporous zeolite has a silica-alumina ratio of greater than 10.

3. The method of claim 1, wherein the mesoporous zeolite is selected from the group consisting of ZSM-type zeolites and ZRP-type zeolites, and the macroporous zeolite is a Y-type zeolite.

4. 2. The process of claim 1, wherein step (2) is carried out such that the resulting reaction product has a propylene / propane mass ratio of 4 or greater, and / or an isobutene / isobutane mass ratio of 1 or greater.

5. 2. The method of claim 1, wherein the heavy feedstock is selected from the group consisting of vacuum residue, inferior atmospheric residue, hydrotreated heavy oil, or any mixture thereof.

6. 2. The method of claim 1, wherein the solvent is selected from the group consisting of propane, butane, pentane, or any mixture thereof.

7. The method according to claim 1, wherein the extraction and separation conditions in the step (1) are a temperature of 10 to 200° C., an operating pressure of 1.0 to 15.0 MPa, and a mass ratio of the solvent to the feedstock oil of 1 to 20.

8. 2. The method of claim 1, wherein the light feedstock used in step (2) is selected from the group consisting of petroleum hydrocarbons, other mineral oils, or mixtures thereof, wherein the petroleum hydrocarbons are selected from the group consisting of vacuum gas oil, atmospheric gas oil, coker gas oil, premium residual oil, premium hydrotreated heavy oil, or any mixtures thereof, and the other mineral oils are selected from the group consisting of coal liquids, tar sands oil, shale oil, or any mixtures thereof.

9. 2. The process of claim 1, wherein the catalytic conversion reactor used in step (2) is a fluidized bed reactor, including a single fluidized bed reactor or a composite reactor comprising a plurality of fluidized bed reactors connected in series or in parallel.

10. The method according to claim 1, wherein the catalytically cracked distillate oil in step (3) has an initial boiling point of 250° C. or higher, a final boiling point of 520° C. or lower, and a hydrogen content of 11.0 wt.% or lower.

11. 2. The process of claim 1, wherein a catalyst comprising a Group VIB metal and / or a Group VIII metal supported on an alumina and / or an amorphous silica-alumina support is used in the hydrodesulfurization step (4).

12. 12. The process according to claim 11, wherein the catalyst used in hydrodesulfurization step (4) comprises 0 to 10% by weight of an additive, 1 to 40% by weight of at least one Group VIII metal (calculated as metal oxide), 1 to 50% by weight of at least one Group VIB metal (calculated as metal oxide), the remainder being a support selected from alumina and amorphous silica-alumina, said additive comprising an element selected from the group consisting of fluorine, phosphorus, titanium, platinum or a combination thereof.

13. The conditions for the hydrodesulfurization treatment (4) are a reaction pressure of 2.0 to 24.0 MPa, a reaction temperature of 200 to 500°C, and a volume ratio of hydrogen to oil of 50 to 5000 Nm ３ / m ３ and the liquid hourly space velocity is 0.1 to 30.0 h －１ The method of claim 1, wherein 14. The method according to claim 1, wherein the conditions of the hydrodesulfurization step (4) are a reaction pressure of 3.0-15.0 MPa, a reaction temperature of 300-400° C., a volume ratio of hydrogen to oil of 200-2000 Nm 3 / m 3 , and a liquid hourly space velocity of 0.2-10.0 h −1 .

15. The method according to claim 1, wherein the hydrodistilled oil obtained in step (4) has a sulfur content of 0.1% or less.

16. 3. The process of claim 2, wherein step (2) is carried out such that the resulting reaction product has a propylene / propane mass ratio of 4 or greater and / or an isobutene / isobutane mass ratio of 1 or greater.

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